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1 CN202511161089 CN202511161089 CN121247965 117305867 CN121247965 A 2026-01-02 [CN121247965] 2025-08-19 2025-08-19 2026-01-02 (CN121247965)|2045-08-19 (CN121247965)|Improved agricultural irrigation water, application method thereof and method for simultaneously realizing preparation, carbon sequestration and mineral weathering acceleration of improved agricultural irrigation water (CN121247965)|The invention discloses improved agricultural irrigation water, an application method thereof and a method for simultaneously realizing preparation, carbon sequestration and mineral weathering acceleration of the improved agricultural irrigation water, and relates to the technical field of agricultural irrigation and carbon sequestration. The method is based on an electrochemical treatment device, the electrochemical treatment device comprises an open reaction tank, an external power supply, an anode, a cathode and a barrier piece, the anode, the cathode and the barrier piece are arranged in the open reaction tank, and the area nearby the anode is used for being filled with minerals; the blocking piece is used for blocking minerals in an area near the anode; the method comprises the following steps: filling mineral into an area near an anode, introducing agricultural irrigation water into an open reaction tank, starting an external power supply for electrolysis, and simultaneously realizing preparation of improved agricultural irrigation water, carbon sequestration and mineral weathering acceleration. The improved agricultural irrigation water is used for agricultural irrigation, can neutralize acidified soil, supplement lost nutrients of the soil, provide required nutrient elements for plants, reduce application of chemical fertilizers and capture carbon dioxide, and has good agricultural benefits and environmental benefits. UNIVERSITY SOUTH SCIENCE & TECHNOLOGY CHINA (CN121247965)|UNIV SOUTH SCIENCE & TECHNOLOGY CHINA ([CN]) LEI YANG|PU YING (CN121247965)|LEI YANG|PU YING (CN121247965)|FAN BING;JOHNSON IP|Reg. Nb: 44268 (CN121247965)|Compared with the prior art, the method has the following technical effects that (1) water resources are not required to be additionally consumed, the efficient utilization of the agricultural irrigation water is realized, the limitation that the agricultural irrigation water is only used as a water supply means is broken through, (2) the improved agricultural irrigation water is rich in nutrient elements and trace elements required by plant growth, nutrients can be provided for crops, fertilizer application is reduced, production cost is lowered, the growth of the crops is promoted, good agricultural benefits are brought, the alkaline characteristics of the improved agricultural irrigation water can effectively neutralize soil acidification, the soil structure is improved, the problem of nutrient loss is relieved, compared with the conventional soil improvement technology, the addition of medicaments and waste materials is reduced, the obvious environmental benefits are brought, mechanical devices such as aeration and the like are avoided, and the problems that the added bicarbonate in the irrigation water can further maintain the stability of the soil pH, the traditional carbon sequestration and carbon capture technology is high in cost and limited in application scene are avoided.|Meanwhile, the agricultural field is facing the problems of soil acidification, nutrient loss, irrigation water quality deterioration and the like.|Traditional carbon sequestration techniques (such as geological sequestration) and carbon capture techniques (amine absorption or physical adsorption) are costly and difficult to apply in agricultural activities.| (CN121247965)|1. A method for simultaneously achieving improved preparation of agricultural irrigation water, carbon sequestration and accelerated mineral weathering, the method being based on an electrochemical treatment device comprising: An open reaction tank; the anode and the cathode are arranged in the open reaction tank at intervals, and the area near the anode is used for filling minerals; The blocking piece is arranged in the open reaction tank and is used for blocking the minerals in the area near the anode; The anode of the external power supply is electrically connected with the cathode, and the cathode of the external power supply is electrically connected with the anode; The method comprises the following steps: Filling minerals into the area near the anode, introducing agricultural irrigation water into the open reaction tank, and starting an external power supply to perform electrolytic reaction; In the process of electrolytic reaction, minerals are weathered with acceleration, the agricultural irrigation water is alkalized, and the alkalized agricultural irrigation water automatically absorbs carbon dioxide in the air; after the electrolytic reaction is finished, improved agricultural irrigation water is obtained in the open reaction tank. | (CN121247965)|Based on the defects in the prior art, the invention aims to provide improved agricultural irrigation water, an application method thereof and a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of the improved agricultural irrigation water, and aims to solve the problems that the existing soil improvement technology needs to additionally add medicaments or conditioning agents, the carbon sealing and carbon capturing technology is high in cost and difficult to apply in agricultural activities, the mineralization rate of the enhanced mineral weathering technology is low, dust pollution and soil hardening risks exist, and the like, and the agricultural irrigation water is further efficiently utilized.|The invention discloses improved agricultural irrigation water, an application method thereof and a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of the improved agricultural irrigation water, and relates to the technical field of agricultural irrigation and carbon fixation.|The invention relates to the technical field of agricultural irrigation and carbon sequestration, in particular to improved agricultural irrigation water, an application method thereof and a method for simultaneously preparing the same, carbon sequestration and accelerating mineral weathering.| (CN121247965)|AGRICULTURAL IRRIGATION(100,131)|AGRICULTURAL IRRIGATION WATER(100,91)|ACCELERATED MINERAL WEATHERING(100,13)|CARBON FIXATION(100,11)|GEOLOGICAL SEQUESTRATION(62,1)|ANODE(56,59)|FILLING MINERAL(53,14)|AGRICULTURAL BENEFIT(47,3)|ALKALIZED AGRICULTURAL IRRIGATION(46,5)|ELECTROLYTIC REACTION(43,14)|BLOCKING MINERAL(42,4)|SOIL HARDENING RISK(41,2)|CATHODE(40,27)|BLOCKING PIECE(40,9)|SUPPLEMENT NUTRIENT(39,1)|OPEN REACTION TANK(38,28)|CONDUCTIVE ROD(37,22)|ELECTROCHEMICAL TREATMENT(36,17)|MODIFIED AGRICULTURAL IRRIGATION(35,10)|SOIL ACIDIFICATION(35,8)|DUST POLLUTION(31,2)|AMINE ABSORPTION(31,1)|NUTRIENT LOSS(29,6)|MINERALIZATION(29,1)|ENHANCED MINERAL WEATHERING(28,2)|MINERAL(27,19)|NUTRIENT(27,14)|FERTILIZER(27,7)|ELECTROLYSIS REACTION(27,4)|CARBON SEQUESTRATION(26,11)|WASTE PHOSPHOGYPSUM(25,3)|MINERAL WEATHERING(24,7)|CARBON SEALING(24,1)|IRRIGATION WATER QUALITY DETERIORATION(23,1)|MEDICAMENT(23,1)|MINERAL LOAD(23,1)|WASTE CONCRETE(22,3)|DEFECT(20,1)|CARBON CAPTURE(19,3)|IRRIGATION WATER(18,5)|SOIL IMPROVEMENT(18,4)|ACCELERATION(18,3)|BICARBONATE ADDITION(18,2)|AERATION(17,2)|CAPTURE CARBON DIOXIDE(17,1)|SCREENING UNDERSIZE OLIVINE PARTICLE(16,2)|SILICATE MINERAL(15,6)|CONDITIONING AGENT(15,1)|LIMESTONE(14,3)|AGRICULTURAL DRAINAGE WATER(14,2)|CROP(14,2)|PHYSICAL ADSORPTION(14,1)|INORGANIC CARBON(13,8)|CARBONATE MINERAL(13,6)|SOLID WASTE MINERAL(13,6)|MAGNESITE(13,3)|DOLOMITE(12,3)|PYROXENE(12,3)|CARBON DIOXIDE(11,29)|ROD SHAPED ANODE(11,7)|PRODUCTION COST(11,3)|SCREENING OLIVINE PARTICLE(11,2)|APPLICATION SCENE(11,1)|CARBON SEQUESTRATION(11,1)|PLANT GROWTH(10,6)|SOIL PH(10,2)|INSULATING MESH MATERIAL(10,1)|ONSCREEN OLIVINE PARTICLE(10,1)|MANGANESE(9,6)|PHOSPHORUS(9,6)|AIR ENVIRONMENT(9,3)|FARM IRRIGATION(9,2)|TRACE ELEMENT(9,1)|COBALT(8,6)|ELECTROCHEMICAL TREATMENT CYLINDRICAL ANODE(8,3)|HEAT EXCHANGER(8,3)|PLANE NET SHAPED ANODE(8,3)|MICROBIAL FERTILIZER INTRODUCTION(8,1)|MESH PORE DIAMETER(7,4)|REGULAR SOIL TILLAGE(7,1)|SLOW MINERAL EFFLORESCENCE(7,1)|UNREASONABLE CULTIVATION(7,1)|CARBON MATERIAL(6,6)|WATER RESOURCE(6,5)|MESH SIEVE(6,3)|SOIL STRUCTURE(6,2)|CROP GROWTH PROMOTER(6,1)|FERTILIZER LEACHING(6,1)|WATER SUPPLY(6,1)|ALKALINE SOLUTION(5,3)|INORGANIC PARTICLE DIAMETER(5,3)|NET MATERIAL(5,3)|RATED CURRENT(5,3)|WATER RESOURCE SHORTAGE(5,3)|CYLINDRICAL CATHODE(5,2)|AGRICULTURAL ECOLOGICAL DEGRADATION(5,1)|AGRICULTURAL FIELD(5,1)|BASIC NUTRIENT LEACHING LOSS(5,1)|FARMLAND IRRIGATION PIPE NETWORK(5,1)|EXTERNAL POWER SUPPLY(4,15)|CHEMICAL COMPONENT(4,3)|WASTE MATERIAL(4,2)|ALKALINE MINERAL(4,1)|CARBONATE PRECIPITATE(4,1)|CYLINDRICAL SIDE(4,1)|DILUTED MODIFIED AGRICULTURAL IRRIGATION(4,1)|CYLINDER OPEN REACTION TANK(3,4)|PARTICLE SIZE(3,4)|ACID RAIN SEDIMENTATION(3,1)|ALKALINE ENVIRONMENT(3,1)|BLOCKING CYLINDER PIECE(3,1)|CYLINDRICAL BARRIER PIECE(3,1)|GYPSUM(3,1)|IRRIGATION STANDARD(3,1)|MESH APERTURE(3,1)|MINERAL DISSOLUTION EFFICIENCY LIMIT(3,1)|NATURAL ROCK FERTILIZER(3,1)|NUTRIENT BASE(3,1)| (CN121247965)|1. A method for simultaneously achieving improved preparation of agricultural irrigation water, carbon sequestration and accelerated mineral weathering, the method being based on an electrochemical treatment device comprising:| An open reaction tank; | the anode and the cathode are arranged in the open reaction tank at intervals, and the area near the anode is used for filling minerals; | The blocking piece is arranged in the open reaction tank and is used for blocking the minerals in the area near the anode; | The anode of the external power supply is electrically connected with the cathode, and the cathode of the external power supply is electrically connected with the anode; | The method comprises the following steps: | Filling minerals into the area near the anode, introducing agricultural irrigation water into the open reaction tank, and starting an external power supply to perform electrolytic reaction; | In the process of electrolytic reaction, minerals are weathered with acceleration, the agricultural irrigation water is alkalized, and the alkalized agricultural irrigation water automatically absorbs carbon dioxide in the air; | after the electrolytic reaction is finished, improved agricultural irrigation water is obtained in the open reaction tank. |2. The method of claim 1, wherein the mineral comprises at least one of a silicate mineral, a carbonate mineral, and a solid waste mineral, and/or,|The particle size of the minerals is 0.1-10 cm, and/or,|The agricultural irrigation water is surface water or agricultural drainage water.|3. The method of claim 2, wherein the silicate mineral comprises at least one of olivine, serpentine, and pyroxene;| the carbonate mineral comprises at least one of limestone, dolomite and magnesite; | the solid waste minerals include at least one of waste concrete and waste phosphogypsum. |4. The method of claim 1, wherein the rated current used for the electrolysis reaction is 0.01-1 a and the time used for the electrolysis reaction is 0.5-5 h.|5. The method according to claim 1, wherein the barrier is an anode, the anode is cylindrical and is used for filling the minerals, the side surface of the cylinder and one end surface are both made of net materials, and the other end surface is open and provided with a first conducting rod; the cathode is cylindrical and concentrically arranged outside the anode, the side surface of the cylinder is made of a net-shaped material, both end surfaces are open, and a second conducting rod is arranged on one end surface;| Or alternatively, the first and second heat exchangers may be, |The anode is in a plane net shape, a space for filling the minerals is formed between the anode and the wall of the open reaction tank, a third conducting rod is arranged on the anode, the cathode is in a plane net shape and is arranged on the opposite side of the anode, a fourth conducting rod is arranged on the cathode, and the step of filling the minerals into the area near the anode is specifically to fill the minerals into the space formed by the plane net-shaped anode and the wall of the open reaction tank.|6. The method of claim 5, wherein the anode is made of metal or carbon material and the cathode is made of metal or carbon material.|7. The method of claim 1, wherein the barrier is cylindrical for loading the mineral, and the cylindrical side and one end are both insulating mesh materials;| The anode is a rod-shaped anode, and the rod-shaped anode is arranged in the barrier; | The cathode is cylindrical, is concentrically arranged outside the barrier, the side surface of the cylinder is made of a net-shaped material, two end surfaces are both open, and one end surface is provided with a second conducting rod. |8. An improved agricultural irrigation water, characterized in that it is obtained by the method according to any one of claims 1 to 7.|9. The modified agricultural irrigation water of claim 8, wherein the modified agricultural irrigation water comprises the following chemical components:| calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt, and inorganic carbon. |10. A method of using the modified agricultural irrigation water according to any of claims 8 to 9, comprising the steps of:| diluting the modified agricultural irrigation water to a pH of more than 5.5 and less than 8.5, and then capturing carbon dioxide in the air while being used for agricultural irrigation, or, |And placing the improved agricultural irrigation water in an air environment to capture carbon dioxide in the air, and continuously capturing carbon dioxide in the air when the pH is reduced to be more than 5.5 and less than 8.5 for agricultural irrigation. (CN121247965)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of agricultural irrigation and carbon sequestration, in particular to improved agricultural irrigation water, an application method thereof and a method for simultaneously preparing the same, carbon sequestration and accelerating mineral weathering.|BACKGROUND ART|[0002] The problem of water resource shortage caused by uneven water resource distribution and over exploitation is increasingly prominent, and the efficient utilization of agricultural irrigation water is beneficial to alleviating the problem of water resource shortage. Meanwhile, the agricultural field is facing the problems of soil acidification, nutrient loss, irrigation water quality deterioration and the like. The factors such as nitrogen fertilizer, acid rain sedimentation and unreasonable cultivation are excessively applied for a long time, so that the cultivated land is acidified to different degrees, agricultural irrigation water (groundwater and river water) is also affected by acid rain and fertilizer leaching, the pH value is reduced, and the soil acidification can be further aggravated after long-term use. The acidified soil not only damages the soil aggregate structure, but also can aggravate leaching loss of basic nutrient elements such as calcium, magnesium, potassium and the like, inhibit microbial activity, and lead to crop yield reduction and quality reduction. To compensate for the loss of nutrients and improve the soil conditions, soil improvement means such as physical (e.g., regular soil tillage, artificial clay addition, etc.), chemical (e.g., lime or gypsum application, fertilizer application, etc.), biological (e.g., composting, introduction of microbial fertilizers, etc.) and the like are generally adopted, but the production cost is further increased. In addition, agricultural activities (e.g., fertilizer application, irrigation energy consumption) are also one of the important contributors to climate change such as an increase in atmospheric carbon dioxide concentration. Traditional carbon sequestration techniques (such as geological sequestration) and carbon capture techniques (amine absorption or physical adsorption) are costly and difficult to apply in agricultural activities.|[0003] Enhanced mineral weathering technology has great potential in facilitating agricultural production and in mitigating climate change. The technology of enhancing mineral weathering is a natural process strengthening technology, crushed alkaline minerals (such as silicate and carbonate) are added into the environment, and the alkaline environment generated in the mineral dissolution process promotes the absorption of carbon dioxide in the atmosphere, so that carbonate precipitates are generated or bicarbonate is formed to be converged into the ocean, and long-term carbon sequestration is realized. For example, rock powder is made into natural rock fertilizer, but the method has the problems of slow mineral efflorescence, high crushing energy consumption, dust pollution, soil hardening risk and the like. For another example, adding minerals to inland water increases alkalinity, but low mineral dissolution efficiency limits carbon removal efficiency.|[0004] Accordingly, the prior art is still in need of improvement and development.|DISCLOSURE|Disclosure of Invention|[0005] Based on the defects in the prior art, the invention aims to provide improved agricultural irrigation water, an application method thereof and a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of the improved agricultural irrigation water, and aims to solve the problems that the existing soil improvement technology needs to additionally add medicaments or conditioning agents, the carbon sealing and carbon capturing technology is high in cost and difficult to apply in agricultural activities, the mineralization rate of the enhanced mineral weathering technology is low, dust pollution and soil hardening risks exist, and the like, and the agricultural irrigation water is further efficiently utilized.|[0006] The technical scheme of the invention is as follows:|[0007] In a first aspect of the invention, there is provided a method for simultaneously effecting the preparation of improved agricultural irrigation water, carbon sequestration and accelerated mineral weathering, wherein the method is based on an electrochemical treatment apparatus comprising: |[0008] An open reaction tank; |[0009] the anode and the cathode are arranged in the open reaction tank at intervals, and the area near the anode is used for filling minerals; |[0010] The blocking piece is arranged in the open reaction tank and is used for blocking the minerals in the area near the anode; |[0011] The anode of the external power supply is electrically connected with the cathode, and the cathode of the external power supply is electrically connected with the anode; |[0012] The method comprises the following steps: |[0013] Filling minerals into the area near the anode, introducing agricultural irrigation water into the open reaction tank, and starting an external power supply to perform electrolytic reaction; |[0014] In the process of electrolytic reaction, minerals are weathered with acceleration, the agricultural irrigation water is alkalized, and the alkalized agricultural irrigation water automatically absorbs carbon dioxide in the air; |[0015] after the electrolytic reaction is finished, improved agricultural irrigation water is obtained in the open reaction tank. |[0016] Optionally, the minerals comprise at least one of silicate minerals, carbonate minerals and solid waste minerals, and/or,|[0017] The particle size of the minerals is 0.1-10 cm, and/or,|[0018] The agricultural irrigation water is surface water or agricultural drainage water.|[0019] Optionally, the silicate mineral comprises at least one of olivine, serpentine, and pyroxene;|[0020] the carbonate mineral comprises at least one of limestone, dolomite and magnesite; |[0021] the solid waste minerals include at least one of waste concrete and waste phosphogypsum. |[0022] Optionally, the rated current adopted by the electrolytic reaction is 0.01-1A, and the time adopted by the electrolytic reaction is 0.5-5 h.|[0023] Optionally, the blocking piece is an anode, the anode is cylindrical and is used for filling the minerals, the side surface of the cylinder and one end surface are both made of net materials, and the other end surface is open and provided with a first conducting rod;|[0024] Or alternatively, the first and second heat exchangers may be, |[0025] The anode is in a plane net shape, a space for filling the minerals is formed between the anode and the wall of the open reaction tank, a third conducting rod is arranged on the anode, the structure of the cathode is the same as that of the anode, the cathode is arranged on the opposite side of the anode, a fourth conducting rod is arranged on the cathode, and the step of filling the minerals into the area near the anode is specifically to fill the minerals into the space formed by the plane net-shaped anode and the wall of the open reaction tank.|[0026] Optionally, the anode is made of metal or carbon material, and the cathode is made of metal or carbon material.|[0027] Optionally, the blocking piece is cylindrical and is used for filling the minerals, and the side surface and one end surface of the cylinder are both made of insulating net materials;|[0028] The anode is a rod-shaped anode, and the rod-shaped anode is arranged in the barrier; |[0029] The cathode is cylindrical, is concentrically arranged outside the barrier, the side surface of the cylinder is made of a net-shaped material, two end surfaces are both open, and one end surface is provided with a second conducting rod. |[0030] In a second aspect of the present invention, there is provided an improved agricultural irrigation water, wherein the improved agricultural irrigation water is obtained by the method of the present invention as described above.|[0031] Optionally, the improved agricultural irrigation water contains the following chemical components:|[0032] calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt, and inorganic carbon. |[0033] In a third aspect of the present invention, there is provided a method of using the modified agricultural irrigation water of the present invention as described above, comprising the steps of:|[0034] diluting the modified agricultural irrigation water to a pH of more than 5.5 and less than 8.5, and then capturing carbon dioxide in the air while being used for agricultural irrigation, or, |[0035] And placing the improved agricultural irrigation water in an air environment to capture carbon dioxide in the air, and continuously capturing carbon dioxide in the air when the pH is reduced to be more than 5.5 and less than 8.5 for agricultural irrigation.|[0036] The invention combines the agricultural irrigation water with the accelerated mineral weathering, introduces the agricultural irrigation water and the minerals into an electrochemical treatment device for electrolysis, and the minerals are accelerated to be weathered by the treatment of the device, so that the agricultural irrigation water is alkalized (the pH value is increased), the alkalized agricultural irrigation water automatically captures carbon dioxide in the air, and the content of nutrient elements such as calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt and the like beneficial to plant growth is increased. The improved agricultural irrigation water obtained after the treatment of the device can be discharged into an irrigation water pipe network to carry out agricultural irrigation, the improved agricultural irrigation water is in direct contact with air in the spraying process, carbon dioxide in the air is further trapped to realize carbon fixation, and meanwhile, after the improved agricultural irrigation water is used for carrying out agricultural irrigation, the soil can be neutralized and acidified, nutrients lost by the soil can be supplemented, and needed nutrient elements are provided for plants. Therefore, the improved agricultural irrigation water can synchronously solve the problems of soil acidification, nutrient loss and carbon sequestration, can also provide nutrient elements required by plant growth, reduces fertilizer application, and provides a new idea for synergistically coping with multiple challenges of the environment.|[0037] Compared with the prior art, the method has the following technical effects that (1) water resources are not required to be additionally consumed, the efficient utilization of the agricultural irrigation water is realized, the limitation that the agricultural irrigation water is only used as a water supply means is broken through, (2) the improved agricultural irrigation water is rich in nutrient elements and trace elements required by plant growth, nutrients can be provided for crops, fertilizer application is reduced, production cost is lowered, the growth of the crops is promoted, good agricultural benefits are brought, the alkaline characteristics of the improved agricultural irrigation water can effectively neutralize soil acidification, the soil structure is improved, the problem of nutrient loss is relieved, compared with the conventional soil improvement technology, the addition of medicaments and waste materials is reduced, the obvious environmental benefits are brought, mechanical devices such as aeration and the like are avoided, and the problems that the added bicarbonate in the irrigation water can further maintain the stability of the soil pH, the traditional carbon sequestration and carbon capture technology is high in cost and limited in application scene are avoided.|DRAWINGS DESCRIPTION|[0038] FIG. 1 is a flow chart of a method provided by the present invention.|[0039] FIG. 2 is a schematic illustration of the present invention for simultaneously effecting improved agricultural irrigation water preparation, carbon sequestration and accelerated mineral weathering.|INVENTION MODE|Detailed Description|[0040] The invention provides improved agricultural irrigation water, an application method thereof and a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering, and aims to make the purposes, technical schemes and effects of the invention clearer and clearer, and the invention is further described in detail below. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0041] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used in the description of the invention herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.|[0042] The terms such as "vertical," "horizontal," "upper," "lower," "left," "right," and the like are used herein for illustrative purposes only and are not meant to be the only embodiment.|[0043] In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.|[0044] If there is a description of "first", "second", etc. in an embodiment of the present invention, the description of "first", "second", etc. is for descriptive purposes only and is not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated.|[0045] The present embodiment provides a method for simultaneously achieving improved preparation of agricultural irrigation water, carbon fixation and accelerated mineral weathering, wherein the method is based on an electrochemical treatment device (in some embodiments, the device is substantially the same as the electrochemical treatment system disclosed in chinese patent No. 114751488A, the main difference being that the reaction tank in the present invention is open, whereas the reaction tank in patent No. CN 114751488A does not define an opening or a seal), the electrochemical treatment device comprising:|[0046] An open reaction tank; |[0047] The anode and the cathode are arranged in the open reaction tank at intervals, and the area near the anode is used for filling minerals (or ore); |[0048] The blocking piece is arranged in the open reaction tank and is used for blocking the minerals in the area near the anode; |[0049] The anode of the external power supply is electrically connected with the cathode, and the cathode of the external power supply is electrically connected with the anode; |[0050] The method comprises the following steps: |[0051] Filling minerals into the area near the anode, introducing agricultural irrigation water into the open reaction tank, and starting an external power supply to perform electrolytic reaction; |[0052] In the process of electrolytic reaction, minerals are weathered with acceleration, the agricultural irrigation water is alkalized, and the alkalized agricultural irrigation water automatically absorbs carbon dioxide in the air; |[0053] after the electrolytic reaction is finished, improved agricultural irrigation water is obtained in the open reaction tank. |[0054] In the electrochemical treatment device provided by the invention, minerals are fixed in the area near the anode through the barrier, the hydrogen ions generated by the anode directly react with the minerals, so that the dissolution of the minerals (namely the weathering of the minerals) is accelerated, and elements such as calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt and the like (each element is released in a positive ion form) are released into the agricultural irrigation water. Meanwhile, hydroxyl ions generated by the cathode accumulate in the agricultural irrigation water, so that the pH of the agricultural irrigation water is raised as a whole (namely, the agricultural irrigation water is alkalized to obtain an alkaline solution), the alkaline solution can promote carbon dioxide in the air to be dissolved into the alkaline solution, and the carbon dioxide is converted into carbonate/bicarbonate ions to be paired with cations in the solution, so that carbon sequestration is realized.|[0055] Thus, as shown in fig. 1 and 2, the present invention combines the accelerated mineral weathering with the agricultural irrigation water, and the minerals are introduced into an electrochemical treatment device for electrolysis, and through the treatment of the device, the minerals are accelerated to be weathered, the agricultural irrigation water is alkalized (the pH is raised), and the alkalized agricultural irrigation water automatically captures carbon dioxide in the air, and the content of nutrient elements such as calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon and cobalt which are beneficial to plant growth is increased. The improved agricultural irrigation water obtained after the treatment by the device can be discharged into an irrigation water pipe network for agricultural irrigation (such as being discharged into a farmland irrigation pipe network for farmland irrigation), and is in direct contact with air in the spraying process, carbon dioxide in the air is further trapped to realize carbon fixation, and meanwhile, after the improved agricultural irrigation water is utilized for agricultural irrigation, the soil can be neutralized and acidified, nutrients lost by the soil are supplemented, and needed nutrient elements are provided for plants. Therefore, the improved agricultural irrigation water can synchronously solve the problems of soil acidification, nutrient loss and carbon sequestration, can also provide nutrient elements required by plant growth, reduces fertilizer application, and provides a new idea for synergistically coping with multiple challenges of the environment.|[0056] The invention provides a method for promoting crop growth and sealing carbon dioxide by improving agricultural irrigation water, which provides an innovative approach for solving multiple challenges such as water resource shortage, agricultural ecological degradation, climate change and the like.|[0057] Therefore, compared with the prior art, the invention has the following technical effects:|[0058] The improved agricultural irrigation water is rich in nutrient elements and microelements required by plant growth, can provide nutrients for crops, reduce fertilizer application, reduce production cost, promote crop growth and bring good agricultural benefits, (3) the alkaline characteristics of the improved agricultural irrigation water can effectively neutralize soil acidification, improve soil structure and relieve nutrient loss, compared with the conventional soil improvement technology, the addition of medicaments and waste materials is reduced, and remarkable environmental benefits are brought, (4) the improved agricultural irrigation water can spontaneously capture carbon dioxide in the air, mechanical devices such as aeration and the like are avoided, and the added bicarbonate in the irrigation water can further maintain the stability of the pH of the soil, so that the problems of high cost, limited application scene and the like of the traditional carbon sequestration and carbon capture technology are avoided. |[0059] In some embodiments, the minerals include at least one of silicate minerals, carbonate minerals, and solid waste minerals, but are not limited thereto.|[0060] In some embodiments, the silicate mineral includes at least one of olivine, serpentine, and pyroxene, but is not limited thereto.|[0061] In some embodiments, the carbonate mineral includes at least one of limestone, dolomite, and magnesite, but is not limited thereto.|[0062] In some embodiments, the solid waste mineral includes at least one of waste concrete and waste phosphogypsum, but is not limited thereto.|[0063] In some embodiments, the particle size of the mineral is 0.1 to 10cm, for example, 1mm, 2mm, 3mm, 4mm, 5mm, 6mm, 7mm, 8mm, 9mm, 1cm, 2cm, 3cm, 4cm, 5cm, 6cm, 7cm, 8cm, 9cm or 10cm, and specifically 1~2mm、1~3mm、1~4mm、2~3mm、2~4mm、3~4mm、4~5mm、5~6mm、6~7mm、7~8mm、8~9mm、9~10mm、1~2cm、2~3cm、3~4cm、4~5cm、5~6cm、6~7cm、7~8cm、8~9cm、9~10cm、1~10cm、2~10cm、3~10cm、4~10cm、5~10cm、6~10cm、7~10cm or 8 to 10cm, and the like.|[0064] In some embodiments, the agricultural irrigation water is surface water (e.g., river water, lake water, etc.) or agricultural drainage.|[0065] In some embodiments, the rated current for the electrolysis reaction is 0.01-1A (e.g., 10mA、20mA、25mA、30mA、35mA、40mA、45mA、50mA、60mA、70mA、80mA、90mA、100mA、200mA、300mA、400mA、500mA、600mA、700mA、800mA、900mA or 1A, etc.), and the time for the electrolysis reaction is 0.5-5 h, e.g., 0.5h, 1h, 2h, 3h, 4h, 5h, etc.|[0066] In some embodiments, the blocking member is an anode, the anode is cylindrical, the side surface and one end surface of the cylinder are both made of mesh materials (the mesh pore diameter is smaller than the mineral particle diameter; the invention does not need to limit the mesh pore diameter of the cathode mesh material, only the mesh pore diameter of the anode mesh material is smaller than the mineral particle diameter, but the mesh pore diameter of the cathode mesh material can be larger than the mineral particle diameter), the other end surface is open and provided with a first conducting rod, the cathode is cylindrical and concentrically arranged outside the anode, the side surface of the cylinder is made of mesh material, both end surfaces are open, and one end surface is provided with a second conducting rod;|[0067] Or alternatively, the first and second heat exchangers may be, |[0068] The anode is in a plane net shape (the mesh aperture is smaller than the particle size of minerals), a space for filling the minerals is formed between the anode and the wall of the open reaction tank, a third conducting rod is arranged on the anode, the cathode is in a plane net shape and is arranged on the opposite side of the anode, a fourth conducting rod is arranged on the cathode, and the step of filling the minerals into the area near the anode is specifically to fill the minerals into the space formed by the plane net-shaped anode and the wall of the open reaction tank.|[0069] In some embodiments, the anode is made of metal or carbon material, and the cathode is made of metal or carbon material.|[0070] The direct current required by the electrolytic reaction is supplied to the electrochemical treatment device through the first conductive rod and the second conductive rod by an external direct current power supply. The direct current required by the electrolytic reaction is supplied to the electrochemical treatment device through the third conductive rod and the fourth conductive rod by an external direct current power supply. In particular, the specific details and structure of the electrochemical treatment device are shown in the chinese patent No. CN 114751488A.|[0071] In the above embodiments, the anode in the device serves as both a barrier and an anode, which causes a part of hydrogen ions generated from the anode to diffuse to the outside, reducing the hydrogen ion utilization rate. Based on this, in some embodiments, the present invention provides further improvements to the barrier and anode. Specifically, the blocking piece is cylindrical and is used for filling the minerals, and the side surface and one end surface of the cylinder are both made of insulating net-shaped materials (such as nylon net);|[0072] the anode is a rod-shaped anode (such as ruthenium-plated iridium-titanium rod) which is arranged in the barrier; |[0073] The cathode is cylindrical, is concentrically arranged outside the barrier, the side surface of the cylinder is made of a net-shaped material, two end surfaces are both open, and one end surface is provided with a second conducting rod. |[0074] In this embodiment, the anode is located at the center of the barrier and is embedded in the mineral, and more hydrogen ions are utilized, i.e., more hydrogen ions preferentially react with the mineral, and the performance is better. The direct current required for the electrolytic reaction is supplied to the electrochemical treatment device through the rod-shaped anode and the second conductive rod by an external direct current power supply.|[0075] The embodiment of the invention also provides improved agricultural irrigation water, wherein the improved agricultural irrigation water is obtained by the method according to the invention.|[0076] Optionally, the improved agricultural irrigation water contains the following chemical components:|[0077] calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt, and inorganic carbon. |[0078] The embodiment of the invention also provides an application method of the improved agricultural irrigation water, which comprises the following steps:|[0079] diluting the modified agricultural irrigation water to a pH of more than 5.5 and less than 8.5, and then capturing carbon dioxide in the air while being used for agricultural irrigation, or, |[0080] And placing the improved agricultural irrigation water in an air environment (namely, in an atmospheric environment) to capture carbon dioxide in the air, and continuously capturing the carbon dioxide in the air when the pH is reduced to be more than 5.5 and less than 8.5 for agricultural irrigation. The invention is further illustrated by the following specific examples.|[0081] In the following examples, as shown in fig. 2, the electrochemical treatment device used includes:|[0082] a cylindrical open reaction tank, the side wall of which is provided with a water inlet and a water outlet; |[0083] the side surface and one end surface of the cylindrical blocking piece are both made of net-shaped materials (the aperture is 0.5mm, and the materials are nylon nets); |[0084] the rod-shaped anode is arranged in the cylindrical barrier piece and is made of ruthenium-plated iridium-titanium rods; |[0085] A cylindrical cathode concentrically arranged outside the cylindrical barrier, wherein the side surface of the cylindrical cathode is made of a net-shaped material (the aperture is 6mm, the material is stainless steel), two end surfaces are both open, and one end surface is provided with a second conductive rod (the material is stainless steel) |[0086] And the anode of the external power supply is connected with the first conducting rod, and the cathode of the external power supply is connected with the second conducting rod.|[0087] Example 1|[0088] The embodiment provides a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of improved agricultural irrigation water, which comprises the following steps:|[0089] (1) The olivine particles were sieved through a 10 mesh sieve (pore size: 2 mm), the undersize olivine particles were sieved through an 18 mesh sieve (pore size: 1 mm), the obtained on-screen olivine particles (i.e., olivine particles obtained after passing through a 10 mesh sieve but without passing through an 18 mesh sieve, i.e., all particles having particle diameters ranging from 1 to 2 mm) were added to a cylindrical anode of an electrochemical treatment apparatus, agricultural irrigation water (the components of which are shown in table 1) was introduced into a cylindrical open reaction tank of the electrochemical treatment apparatus, the mineral weathering process was accelerated by the electrochemical apparatus, the rated current was set to 20mA, and the electrolysis time was 1h. And (3) starting an external direct current power supply to electrolyze, and obtaining the effluent which is the improved agricultural irrigation water. |[0090] (2) The modified agricultural irrigation water is placed under air environmental conditions and automatically traps (or absorbs) carbon dioxide in the air.|[0091] The components of the agricultural irrigation water and the modified agricultural irrigation water after capturing carbon dioxide in the air are shown in table 1.|[0092] Table 1, parameters of different irrigation waters in example 1|[0093] |[0094] It can be seen that the pH of the modified agricultural irrigation water obtained by the method of this example was 10.6, and the modified agricultural irrigation water containing nutrients required by plants such as magnesium, calcium, silicon and iron increased by 4.8mg C/L (i.e., 4.8mg carbon per liter) as compared to the original agricultural irrigation water. The pH of the improved agricultural irrigation water is reduced to 8.1 after the improved agricultural irrigation water automatically absorbs carbon dioxide in the air, and the inorganic carbon is increased to 18.4mg C/L, so that the improved agricultural irrigation water meets the 'water quality standard for farm irrigation'.|[0095] Example 2|[0096] The embodiment provides a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of improved agricultural irrigation water, which comprises the following steps:|[0097] (1) The method comprises the steps of screening olivine particles through a 10-mesh sieve (aperture is 2 mm), screening undersize olivine particles through an 18-mesh sieve (aperture is 1 mm), adding the obtained undersize olivine particles (all particle diameters are within a range of 1-2 mm) into a cylindrical anode of an electrochemical treatment device, introducing agricultural irrigation water (the components of which are shown in table 2) into a cylindrical open reaction tank of the electrochemical treatment device, accelerating mineral weathering process through the electrochemical device, setting rated current to be 50mA, and setting electrolysis time to be 1h. And (5) starting an external power supply to electrolyze, and obtaining the water which is the improved agricultural irrigation water. |[0098] (2) The modified agricultural irrigation water is placed under air environmental conditions and automatically traps (or absorbs) carbon dioxide in the air.|[0099] The components of the agricultural irrigation water and the modified agricultural irrigation water after capturing carbon dioxide in the air are shown in table 2.|[0100] Table 2, parameters of different irrigation waters in example 2|[0101] |[0102] It can be seen that the pH of the modified agricultural irrigation water obtained by the method of this example was 10.8, and the modified agricultural irrigation water contained nutrients required for plants such as magnesium, calcium, silicon and iron, and the inorganic carbon in the modified agricultural irrigation water obtained after modification was increased by 8.3mg C/L as compared with the original agricultural irrigation water. The pH of the improved agricultural irrigation water is reduced to 8.2 after the improved agricultural irrigation water automatically absorbs carbon dioxide in the air, and the inorganic carbon is increased to 21.8mg C/L, so that the improved agricultural irrigation water meets the 'water quality standard for farm irrigation'.|[0103] Example 3|[0104] The embodiment provides a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of improved agricultural irrigation water, which comprises the following steps:|[0105] (1) The method comprises the steps of screening olivine particles through a 10-mesh sieve (aperture is 2 mm), screening undersize olivine particles through an 18-mesh sieve (aperture is 1 mm), adding the obtained undersize olivine particles (all particle diameters are within a range of 1-2 mm) into a cylindrical anode of an electrochemical treatment device, introducing agricultural irrigation water (the components of which are shown in table 3) into a cylindrical open reaction tank of the electrochemical treatment device, accelerating mineral weathering process through the electrochemical device, setting rated current to be 20mA, and setting electrolysis time to be 1h. And (5) starting an external power supply to electrolyze, and obtaining the water which is the improved agricultural irrigation water. |[0106] (2) The modified agricultural irrigation water is diluted with water so that the pH reaches the irrigation standard (5.5 < pH < 8.5), and the diluted modified agricultural irrigation water obtained is placed under air environmental conditions to trap (or absorb) carbon dioxide in the air.|[0107] Various parameters of the agricultural irrigation water, the modified agricultural irrigation water, the diluted modified agricultural irrigation water, and the diluted modified agricultural irrigation water after capturing carbon dioxide in the air are shown in table 3.|[0108] Table 3, parameters of different irrigation waters in example 3|[0109] |[0110] The pH of the improved agricultural irrigation water obtained by the method of the example was 10.1, and the pH of the improved agricultural irrigation water contained nutrient elements required for plants such as magnesium, calcium, silicon and iron, and the inorganic carbon in the improved agricultural irrigation water obtained after improvement was increased by 7.3mg C/L as compared with the original agricultural irrigation water. The improved agricultural irrigation water is diluted, and the pH value of the diluted improved agricultural irrigation water is 8.5, so that the diluted improved agricultural irrigation water can be directly used for farmland irrigation. The pH of the diluted and improved agricultural irrigation water automatically absorbs carbon dioxide in the air and then drops to 8.1, and the inorganic carbon is increased by 4.8mg C/L.|[0111] It is to be understood that the invention is not limited in its application to the examples described above, but is capable of modification and variation in light of the above teachings by those skilled in the art, and that all such modifications and variations are intended to be included within the scope of the appended claims. (CN121247965)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of agricultural irrigation and carbon sequestration, in particular to improved agricultural irrigation water, an application method thereof and a method for simultaneously preparing the same, carbon sequestration and accelerating mineral weathering.|BACKGROUND ART|[0002] The problem of water resource shortage caused by uneven water resource distribution and over exploitation is increasingly prominent, and the efficient utilization of agricultural irrigation water is beneficial to alleviating the problem of water resource shortage. Meanwhile, the agricultural field is facing the problems of soil acidification, nutrient loss, irrigation water quality deterioration and the like. The factors such as nitrogen fertilizer, acid rain sedimentation and unreasonable cultivation are excessively applied for a long time, so that the cultivated land is acidified to different degrees, agricultural irrigation water (groundwater and river water) is also affected by acid rain and fertilizer leaching, the pH value is reduced, and the soil acidification can be further aggravated after long-term use. The acidified soil not only damages the soil aggregate structure, but also can aggravate leaching loss of basic nutrient elements such as calcium, magnesium, potassium and the like, inhibit microbial activity, and lead to crop yield reduction and quality reduction. To compensate for the loss of nutrients and improve the soil conditions, soil improvement means such as physical (e.g., regular soil tillage, artificial clay addition, etc.), chemical (e.g., lime or gypsum application, fertilizer application, etc.), biological (e.g., composting, introduction of microbial fertilizers, etc.) and the like are generally adopted, but the production cost is further increased. In addition, agricultural activities (e.g., fertilizer application, irrigation energy consumption) are also one of the important contributors to climate change such as an increase in atmospheric carbon dioxide concentration. Traditional carbon sequestration techniques (such as geological sequestration) and carbon capture techniques (amine absorption or physical adsorption) are costly and difficult to apply in agricultural activities.|[0003] Enhanced mineral weathering technology has great potential in facilitating agricultural production and in mitigating climate change. The technology of enhancing mineral weathering is a natural process strengthening technology, crushed alkaline minerals (such as silicate and carbonate) are added into the environment, and the alkaline environment generated in the mineral dissolution process promotes the absorption of carbon dioxide in the atmosphere, so that carbonate precipitates are generated or bicarbonate is formed to be converged into the ocean, and long-term carbon sequestration is realized. For example, rock powder is made into natural rock fertilizer, but the method has the problems of slow mineral efflorescence, high crushing energy consumption, dust pollution, soil hardening risk and the like. For another example, adding minerals to inland water increases alkalinity, but low mineral dissolution efficiency limits carbon removal efficiency.|[0004] Accordingly, the prior art is still in need of improvement and development.|DISCLOSURE|Disclosure of Invention|[0005] Based on the defects in the prior art, the invention aims to provide improved agricultural irrigation water, an application method thereof and a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of the improved agricultural irrigation water, and aims to solve the problems that the existing soil improvement technology needs to additionally add medicaments or conditioning agents, the carbon sealing and carbon capturing technology is high in cost and difficult to apply in agricultural activities, the mineralization rate of the enhanced mineral weathering technology is low, dust pollution and soil hardening risks exist, and the like, and the agricultural irrigation water is further efficiently utilized.|[0006] The technical scheme of the invention is as follows:|[0007] In a first aspect of the invention, there is provided a method for simultaneously effecting the preparation of improved agricultural irrigation water, carbon sequestration and accelerated mineral weathering, wherein the method is based on an electrochemical treatment apparatus comprising: |[0008] An open reaction tank; |[0009] the anode and the cathode are arranged in the open reaction tank at intervals, and the area near the anode is used for filling minerals; |[0010] The blocking piece is arranged in the open reaction tank and is used for blocking the minerals in the area near the anode; |[0011] The anode of the external power supply is electrically connected with the cathode, and the cathode of the external power supply is electrically connected with the anode; |[0012] The method comprises the following steps: |[0013] Filling minerals into the area near the anode, introducing agricultural irrigation water into the open reaction tank, and starting an external power supply to perform electrolytic reaction; |[0014] In the process of electrolytic reaction, minerals are weathered with acceleration, the agricultural irrigation water is alkalized, and the alkalized agricultural irrigation water automatically absorbs carbon dioxide in the air; |[0015] after the electrolytic reaction is finished, improved agricultural irrigation water is obtained in the open reaction tank. |[0016] Optionally, the minerals comprise at least one of silicate minerals, carbonate minerals and solid waste minerals, and/or,|[0017] The particle size of the minerals is 0.1-10 cm, and/or,|[0018] The agricultural irrigation water is surface water or agricultural drainage water.|[0019] Optionally, the silicate mineral comprises at least one of olivine, serpentine, and pyroxene;|[0020] the carbonate mineral comprises at least one of limestone, dolomite and magnesite; |[0021] the solid waste minerals include at least one of waste concrete and waste phosphogypsum. |[0022] Optionally, the rated current adopted by the electrolytic reaction is 0.01-1A, and the time adopted by the electrolytic reaction is 0.5-5 h.|[0023] Optionally, the blocking piece is an anode, the anode is cylindrical and is used for filling the minerals, the side surface of the cylinder and one end surface are both made of net materials, and the other end surface is open and provided with a first conducting rod;|[0024] Or alternatively, the first and second heat exchangers may be, |[0025] The anode is in a plane net shape, a space for filling the minerals is formed between the anode and the wall of the open reaction tank, a third conducting rod is arranged on the anode, the structure of the cathode is the same as that of the anode, the cathode is arranged on the opposite side of the anode, a fourth conducting rod is arranged on the cathode, and the step of filling the minerals into the area near the anode is specifically to fill the minerals into the space formed by the plane net-shaped anode and the wall of the open reaction tank.|[0026] Optionally, the anode is made of metal or carbon material, and the cathode is made of metal or carbon material.|[0027] Optionally, the blocking piece is cylindrical and is used for filling the minerals, and the side surface and one end surface of the cylinder are both made of insulating net materials;|[0028] The anode is a rod-shaped anode, and the rod-shaped anode is arranged in the barrier; |[0029] The cathode is cylindrical, is concentrically arranged outside the barrier, the side surface of the cylinder is made of a net-shaped material, two end surfaces are both open, and one end surface is provided with a second conducting rod. |[0030] In a second aspect of the present invention, there is provided an improved agricultural irrigation water, wherein the improved agricultural irrigation water is obtained by the method of the present invention as described above.|[0031] Optionally, the improved agricultural irrigation water contains the following chemical components:|[0032] calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt, and inorganic carbon. |[0033] In a third aspect of the present invention, there is provided a method of using the modified agricultural irrigation water of the present invention as described above, comprising the steps of:|[0034] diluting the modified agricultural irrigation water to a pH of more than 5.5 and less than 8.5, and then capturing carbon dioxide in the air while being used for agricultural irrigation, or, |[0035] And placing the improved agricultural irrigation water in an air environment to capture carbon dioxide in the air, and continuously capturing carbon dioxide in the air when the pH is reduced to be more than 5.5 and less than 8.5 for agricultural irrigation.|[0036] The invention combines the agricultural irrigation water with the accelerated mineral weathering, introduces the agricultural irrigation water and the minerals into an electrochemical treatment device for electrolysis, and the minerals are accelerated to be weathered by the treatment of the device, so that the agricultural irrigation water is alkalized (the pH value is increased), the alkalized agricultural irrigation water automatically captures carbon dioxide in the air, and the content of nutrient elements such as calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt and the like beneficial to plant growth is increased. The improved agricultural irrigation water obtained after the treatment of the device can be discharged into an irrigation water pipe network to carry out agricultural irrigation, the improved agricultural irrigation water is in direct contact with air in the spraying process, carbon dioxide in the air is further trapped to realize carbon fixation, and meanwhile, after the improved agricultural irrigation water is used for carrying out agricultural irrigation, the soil can be neutralized and acidified, nutrients lost by the soil can be supplemented, and needed nutrient elements are provided for plants. Therefore, the improved agricultural irrigation water can synchronously solve the problems of soil acidification, nutrient loss and carbon sequestration, can also provide nutrient elements required by plant growth, reduces fertilizer application, and provides a new idea for synergistically coping with multiple challenges of the environment.|[0037] Compared with the prior art, the method has the following technical effects that (1) water resources are not required to be additionally consumed, the efficient utilization of the agricultural irrigation water is realized, the limitation that the agricultural irrigation water is only used as a water supply means is broken through, (2) the improved agricultural irrigation water is rich in nutrient elements and trace elements required by plant growth, nutrients can be provided for crops, fertilizer application is reduced, production cost is lowered, the growth of the crops is promoted, good agricultural benefits are brought, the alkaline characteristics of the improved agricultural irrigation water can effectively neutralize soil acidification, the soil structure is improved, the problem of nutrient loss is relieved, compared with the conventional soil improvement technology, the addition of medicaments and waste materials is reduced, the obvious environmental benefits are brought, mechanical devices such as aeration and the like are avoided, and the problems that the added bicarbonate in the irrigation water can further maintain the stability of the soil pH, the traditional carbon sequestration and carbon capture technology is high in cost and limited in application scene are avoided.|DRAWINGS DESCRIPTION|[0038] FIG. 1 is a flow chart of a method provided by the present invention.|[0039] FIG. 2 is a schematic illustration of the present invention for simultaneously effecting improved agricultural irrigation water preparation, carbon sequestration and accelerated mineral weathering.|INVENTION MODE|Detailed Description|[0040] The invention provides improved agricultural irrigation water, an application method thereof and a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering, and aims to make the purposes, technical schemes and effects of the invention clearer and clearer, and the invention is further described in detail below. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0041] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used in the description of the invention herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.|[0042] The terms such as "vertical," "horizontal," "upper," "lower," "left," "right," and the like are used herein for illustrative purposes only and are not meant to be the only embodiment.|[0043] In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.|[0044] If there is a description of "first", "second", etc. in an embodiment of the present invention, the description of "first", "second", etc. is for descriptive purposes only and is not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated.|[0045] The present embodiment provides a method for simultaneously achieving improved preparation of agricultural irrigation water, carbon fixation and accelerated mineral weathering, wherein the method is based on an electrochemical treatment device (in some embodiments, the device is substantially the same as the electrochemical treatment system disclosed in chinese patent No. 114751488A, the main difference being that the reaction tank in the present invention is open, whereas the reaction tank in patent No. CN 114751488A does not define an opening or a seal), the electrochemical treatment device comprising:|[0046] An open reaction tank; |[0047] The anode and the cathode are arranged in the open reaction tank at intervals, and the area near the anode is used for filling minerals (or ore); |[0048] The blocking piece is arranged in the open reaction tank and is used for blocking the minerals in the area near the anode; |[0049] The anode of the external power supply is electrically connected with the cathode, and the cathode of the external power supply is electrically connected with the anode; |[0050] The method comprises the following steps: |[0051] Filling minerals into the area near the anode, introducing agricultural irrigation water into the open reaction tank, and starting an external power supply to perform electrolytic reaction; |[0052] In the process of electrolytic reaction, minerals are weathered with acceleration, the agricultural irrigation water is alkalized, and the alkalized agricultural irrigation water automatically absorbs carbon dioxide in the air; |[0053] after the electrolytic reaction is finished, improved agricultural irrigation water is obtained in the open reaction tank. |[0054] In the electrochemical treatment device provided by the invention, minerals are fixed in the area near the anode through the barrier, the hydrogen ions generated by the anode directly react with the minerals, so that the dissolution of the minerals (namely the weathering of the minerals) is accelerated, and elements such as calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt and the like (each element is released in a positive ion form) are released into the agricultural irrigation water. Meanwhile, hydroxyl ions generated by the cathode accumulate in the agricultural irrigation water, so that the pH of the agricultural irrigation water is raised as a whole (namely, the agricultural irrigation water is alkalized to obtain an alkaline solution), the alkaline solution can promote carbon dioxide in the air to be dissolved into the alkaline solution, and the carbon dioxide is converted into carbonate/bicarbonate ions to be paired with cations in the solution, so that carbon sequestration is realized.|[0055] Thus, as shown in fig. 1 and 2, the present invention combines the accelerated mineral weathering with the agricultural irrigation water, and the minerals are introduced into an electrochemical treatment device for electrolysis, and through the treatment of the device, the minerals are accelerated to be weathered, the agricultural irrigation water is alkalized (the pH is raised), and the alkalized agricultural irrigation water automatically captures carbon dioxide in the air, and the content of nutrient elements such as calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon and cobalt which are beneficial to plant growth is increased. The improved agricultural irrigation water obtained after the treatment by the device can be discharged into an irrigation water pipe network for agricultural irrigation (such as being discharged into a farmland irrigation pipe network for farmland irrigation), and is in direct contact with air in the spraying process, carbon dioxide in the air is further trapped to realize carbon fixation, and meanwhile, after the improved agricultural irrigation water is utilized for agricultural irrigation, the soil can be neutralized and acidified, nutrients lost by the soil are supplemented, and needed nutrient elements are provided for plants. Therefore, the improved agricultural irrigation water can synchronously solve the problems of soil acidification, nutrient loss and carbon sequestration, can also provide nutrient elements required by plant growth, reduces fertilizer application, and provides a new idea for synergistically coping with multiple challenges of the environment.|[0056] The invention provides a method for promoting crop growth and sealing carbon dioxide by improving agricultural irrigation water, which provides an innovative approach for solving multiple challenges such as water resource shortage, agricultural ecological degradation, climate change and the like.|[0057] Therefore, compared with the prior art, the invention has the following technical effects:|[0058] The improved agricultural irrigation water is rich in nutrient elements and microelements required by plant growth, can provide nutrients for crops, reduce fertilizer application, reduce production cost, promote crop growth and bring good agricultural benefits, (3) the alkaline characteristics of the improved agricultural irrigation water can effectively neutralize soil acidification, improve soil structure and relieve nutrient loss, compared with the conventional soil improvement technology, the addition of medicaments and waste materials is reduced, and remarkable environmental benefits are brought, (4) the improved agricultural irrigation water can spontaneously capture carbon dioxide in the air, mechanical devices such as aeration and the like are avoided, and the added bicarbonate in the irrigation water can further maintain the stability of the pH of the soil, so that the problems of high cost, limited application scene and the like of the traditional carbon sequestration and carbon capture technology are avoided. |[0059] In some embodiments, the minerals include at least one of silicate minerals, carbonate minerals, and solid waste minerals, but are not limited thereto.|[0060] In some embodiments, the silicate mineral includes at least one of olivine, serpentine, and pyroxene, but is not limited thereto.|[0061] In some embodiments, the carbonate mineral includes at least one of limestone, dolomite, and magnesite, but is not limited thereto.|[0062] In some embodiments, the solid waste mineral includes at least one of waste concrete and waste phosphogypsum, but is not limited thereto.|[0063] In some embodiments, the particle size of the mineral is 0.1 to 10cm, for example, 1mm, 2mm, 3mm, 4mm, 5mm, 6mm, 7mm, 8mm, 9mm, 1cm, 2cm, 3cm, 4cm, 5cm, 6cm, 7cm, 8cm, 9cm or 10cm, and specifically 1~2mm、1~3mm、1~4mm、2~3mm、2~4mm、3~4mm、4~5mm、5~6mm、6~7mm、7~8mm、8~9mm、9~10mm、1~2cm、2~3cm、3~4cm、4~5cm、5~6cm、6~7cm、7~8cm、8~9cm、9~10cm、1~10cm、2~10cm、3~10cm、4~10cm、5~10cm、6~10cm、7~10cm or 8 to 10cm, and the like.|[0064] In some embodiments, the agricultural irrigation water is surface water (e.g., river water, lake water, etc.) or agricultural drainage.|[0065] In some embodiments, the rated current for the electrolysis reaction is 0.01-1A (e.g., 10mA、20mA、25mA、30mA、35mA、40mA、45mA、50mA、60mA、70mA、80mA、90mA、100mA、200mA、300mA、400mA、500mA、600mA、700mA、800mA、900mA or 1A, etc.), and the time for the electrolysis reaction is 0.5-5 h, e.g., 0.5h, 1h, 2h, 3h, 4h, 5h, etc.|[0066] In some embodiments, the blocking member is an anode, the anode is cylindrical, the side surface and one end surface of the cylinder are both made of mesh materials (the mesh pore diameter is smaller than the mineral particle diameter; the invention does not need to limit the mesh pore diameter of the cathode mesh material, only the mesh pore diameter of the anode mesh material is smaller than the mineral particle diameter, but the mesh pore diameter of the cathode mesh material can be larger than the mineral particle diameter), the other end surface is open and provided with a first conducting rod, the cathode is cylindrical and concentrically arranged outside the anode, the side surface of the cylinder is made of mesh material, both end surfaces are open, and one end surface is provided with a second conducting rod;|[0067] Or alternatively, the first and second heat exchangers may be, |[0068] The anode is in a plane net shape (the mesh aperture is smaller than the particle size of minerals), a space for filling the minerals is formed between the anode and the wall of the open reaction tank, a third conducting rod is arranged on the anode, the cathode is in a plane net shape and is arranged on the opposite side of the anode, a fourth conducting rod is arranged on the cathode, and the step of filling the minerals into the area near the anode is specifically to fill the minerals into the space formed by the plane net-shaped anode and the wall of the open reaction tank.|[0069] In some embodiments, the anode is made of metal or carbon material, and the cathode is made of metal or carbon material.|[0070] The direct current required by the electrolytic reaction is supplied to the electrochemical treatment device through the first conductive rod and the second conductive rod by an external direct current power supply. The direct current required by the electrolytic reaction is supplied to the electrochemical treatment device through the third conductive rod and the fourth conductive rod by an external direct current power supply. In particular, the specific details and structure of the electrochemical treatment device are shown in the chinese patent No. CN 114751488A.|[0071] In the above embodiments, the anode in the device serves as both a barrier and an anode, which causes a part of hydrogen ions generated from the anode to diffuse to the outside, reducing the hydrogen ion utilization rate. Based on this, in some embodiments, the present invention provides further improvements to the barrier and anode. Specifically, the blocking piece is cylindrical and is used for filling the minerals, and the side surface and one end surface of the cylinder are both made of insulating net-shaped materials (such as nylon net);|[0072] the anode is a rod-shaped anode (such as ruthenium-plated iridium-titanium rod) which is arranged in the barrier; |[0073] The cathode is cylindrical, is concentrically arranged outside the barrier, the side surface of the cylinder is made of a net-shaped material, two end surfaces are both open, and one end surface is provided with a second conducting rod. |[0074] In this embodiment, the anode is located at the center of the barrier and is embedded in the mineral, and more hydrogen ions are utilized, i.e., more hydrogen ions preferentially react with the mineral, and the performance is better. The direct current required for the electrolytic reaction is supplied to the electrochemical treatment device through the rod-shaped anode and the second conductive rod by an external direct current power supply.|[0075] The embodiment of the invention also provides improved agricultural irrigation water, wherein the improved agricultural irrigation water is obtained by the method according to the invention.|[0076] Optionally, the improved agricultural irrigation water contains the following chemical components:|[0077] calcium, magnesium, phosphorus, potassium, iron, manganese, copper, zinc, silicon, cobalt, and inorganic carbon. |[0078] The embodiment of the invention also provides an application method of the improved agricultural irrigation water, which comprises the following steps:|[0079] diluting the modified agricultural irrigation water to a pH of more than 5.5 and less than 8.5, and then capturing carbon dioxide in the air while being used for agricultural irrigation, or, |[0080] And placing the improved agricultural irrigation water in an air environment (namely, in an atmospheric environment) to capture carbon dioxide in the air, and continuously capturing the carbon dioxide in the air when the pH is reduced to be more than 5.5 and less than 8.5 for agricultural irrigation. The invention is further illustrated by the following specific examples.|[0081] In the following examples, as shown in fig. 2, the electrochemical treatment device used includes:|[0082] a cylindrical open reaction tank, the side wall of which is provided with a water inlet and a water outlet; |[0083] the side surface and one end surface of the cylindrical blocking piece are both made of net-shaped materials (the aperture is 0.5mm, and the materials are nylon nets); |[0084] the rod-shaped anode is arranged in the cylindrical barrier piece and is made of ruthenium-plated iridium-titanium rods; |[0085] A cylindrical cathode concentrically arranged outside the cylindrical barrier, wherein the side surface of the cylindrical cathode is made of a net-shaped material (the aperture is 6mm, the material is stainless steel), two end surfaces are both open, and one end surface is provided with a second conductive rod (the material is stainless steel) |[0086] And the anode of the external power supply is connected with the first conducting rod, and the cathode of the external power supply is connected with the second conducting rod.|[0087] Example 1|[0088] The embodiment provides a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of improved agricultural irrigation water, which comprises the following steps:|[0089] (1) The olivine particles were sieved through a 10 mesh sieve (pore size: 2 mm), the undersize olivine particles were sieved through an 18 mesh sieve (pore size: 1 mm), the obtained on-screen olivine particles (i.e., olivine particles obtained after passing through a 10 mesh sieve but without passing through an 18 mesh sieve, i.e., all particles having particle diameters ranging from 1 to 2 mm) were added to a cylindrical anode of an electrochemical treatment apparatus, agricultural irrigation water (the components of which are shown in table 1) was introduced into a cylindrical open reaction tank of the electrochemical treatment apparatus, the mineral weathering process was accelerated by the electrochemical apparatus, the rated current was set to 20mA, and the electrolysis time was 1h. And (3) starting an external direct current power supply to electrolyze, and obtaining the effluent which is the improved agricultural irrigation water. |[0090] (2) The modified agricultural irrigation water is placed under air environmental conditions and automatically traps (or absorbs) carbon dioxide in the air.|[0091] The components of the agricultural irrigation water and the modified agricultural irrigation water after capturing carbon dioxide in the air are shown in table 1.|[0092] Table 1, parameters of different irrigation waters in example 1|[0093] |[0094] It can be seen that the pH of the modified agricultural irrigation water obtained by the method of this example was 10.6, and the modified agricultural irrigation water containing nutrients required by plants such as magnesium, calcium, silicon and iron increased by 4.8mg C/L (i.e., 4.8mg carbon per liter) as compared to the original agricultural irrigation water. The pH of the improved agricultural irrigation water is reduced to 8.1 after the improved agricultural irrigation water automatically absorbs carbon dioxide in the air, and the inorganic carbon is increased to 18.4mg C/L, so that the improved agricultural irrigation water meets the 'water quality standard for farm irrigation'.|[0095] Example 2|[0096] The embodiment provides a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of improved agricultural irrigation water, which comprises the following steps:|[0097] (1) The method comprises the steps of screening olivine particles through a 10-mesh sieve (aperture is 2 mm), screening undersize olivine particles through an 18-mesh sieve (aperture is 1 mm), adding the obtained undersize olivine particles (all particle diameters are within a range of 1-2 mm) into a cylindrical anode of an electrochemical treatment device, introducing agricultural irrigation water (the components of which are shown in table 2) into a cylindrical open reaction tank of the electrochemical treatment device, accelerating mineral weathering process through the electrochemical device, setting rated current to be 50mA, and setting electrolysis time to be 1h. And (5) starting an external power supply to electrolyze, and obtaining the water which is the improved agricultural irrigation water. |[0098] (2) The modified agricultural irrigation water is placed under air environmental conditions and automatically traps (or absorbs) carbon dioxide in the air.|[0099] The components of the agricultural irrigation water and the modified agricultural irrigation water after capturing carbon dioxide in the air are shown in table 2.|[0100] Table 2, parameters of different irrigation waters in example 2|[0101] |[0102] It can be seen that the pH of the modified agricultural irrigation water obtained by the method of this example was 10.8, and the modified agricultural irrigation water contained nutrients required for plants such as magnesium, calcium, silicon and iron, and the inorganic carbon in the modified agricultural irrigation water obtained after modification was increased by 8.3mg C/L as compared with the original agricultural irrigation water. The pH of the improved agricultural irrigation water is reduced to 8.2 after the improved agricultural irrigation water automatically absorbs carbon dioxide in the air, and the inorganic carbon is increased to 21.8mg C/L, so that the improved agricultural irrigation water meets the 'water quality standard for farm irrigation'.|[0103] Example 3|[0104] The embodiment provides a method for simultaneously realizing preparation, carbon fixation and accelerated mineral weathering of improved agricultural irrigation water, which comprises the following steps:|[0105] (1) The method comprises the steps of screening olivine particles through a 10-mesh sieve (aperture is 2 mm), screening undersize olivine particles through an 18-mesh sieve (aperture is 1 mm), adding the obtained undersize olivine particles (all particle diameters are within a range of 1-2 mm) into a cylindrical anode of an electrochemical treatment device, introducing agricultural irrigation water (the components of which are shown in table 3) into a cylindrical open reaction tank of the electrochemical treatment device, accelerating mineral weathering process through the electrochemical device, setting rated current to be 20mA, and setting electrolysis time to be 1h. And (5) starting an external power supply to electrolyze, and obtaining the water which is the improved agricultural irrigation water. |[0106] (2) The modified agricultural irrigation water is diluted with water so that the pH reaches the irrigation standard (5.5 < pH < 8.5), and the diluted modified agricultural irrigation water obtained is placed under air environmental conditions to trap (or absorb) carbon dioxide in the air.|[0107] Various parameters of the agricultural irrigation water, the modified agricultural irrigation water, the diluted modified agricultural irrigation water, and the diluted modified agricultural irrigation water after capturing carbon dioxide in the air are shown in table 3.|[0108] Table 3, parameters of different irrigation waters in example 3|[0109] |[0110] The pH of the improved agricultural irrigation water obtained by the method of the example was 10.1, and the pH of the improved agricultural irrigation water contained nutrient elements required for plants such as magnesium, calcium, silicon and iron, and the inorganic carbon in the improved agricultural irrigation water obtained after improvement was increased by 7.3mg C/L as compared with the original agricultural irrigation water. The improved agricultural irrigation water is diluted, and the pH value of the diluted improved agricultural irrigation water is 8.5, so that the diluted improved agricultural irrigation water can be directly used for farmland irrigation. The pH of the diluted and improved agricultural irrigation water automatically absorbs carbon dioxide in the air and then drops to 8.1, and the inorganic carbon is increased by 4.8mg C/L.|[0111] It is to be understood that the invention is not limited in its application to the examples described above, but is capable of modification and variation in light of the above teachings by those skilled in the art, and that all such modifications and variations are intended to be included within the scope of the appended claims. Family Number|(117305867)|117305867|Abstract|(CN121247965 A)|The invention discloses improved agricultural irrigation water , an application method thereof and a method for simultaneously realizing preparation , carbon sequestration and mineral weathering acceleration of the improved agricultural irrigation water , and relates to the technical field of agricultural irrigation and carbon sequestration . The method is based on an electrochemical treatment device , the electrochemical treatment device comprises an open reaction tank , an external power supply , an anode , a cathode and a barrier piece , the anode , the cathode and the barrier piece are arranged in the open reaction tank , and the area nearby the anode is used for being filled with minerals ; the blocking piece is used for blocking minerals in an area near the anode ; the method comprises the following steps : filling mineral into an area near an anode , introducing agricultural irrigation water into an open reaction tank , starting an external power supply for electrolysis , and simultaneously realizing preparation of improved agricultural irrigation water , carbon sequestration and mineral weathering acceleration . The improved agricultural irrigation water is used for agricultural irrigation , can neutralize acidified soil , supplement lost nutrients of the soil , provide required nutrient elements for plants , reduce application of chemical fertilizers and capture carbon dioxide , and has good agricultural benefits and environmental benefits . |CPC codes|(CN121247965 A)|A01G - 025/00 |B01D - 053/62 |B01D - 053/78 |B01D - 2257/504 |IPC codes|(CN121247965 A)|A01G - 025/00 |B01D - 053/62 |B01D - 053/78 |Title|(CN121247965 A)|Improved agricultural irrigation water , application method thereof and method for simultaneously realizing preparation , carbon sequestration and mineral weathering acceleration of improved agricultural irrigation water | Basic materials chemistry|Environmental technology|Other special machines A01G-025/02|B01D-029/03|B01D-046/00/36|B01D-050/00/4|B01D-053/04|B01D-053/26|B01D-053/60|B01D-053/62|B01D-053/78|B01D-053/94/09|B01D-2251/50|B01D-2251/61|B01D-2257/504|B01D-2258/0283|B01D-2258/06|B01F-007/18|B01F-015/06/6|B01J-019/00/66|B01J-019/18|B01J-020/26/2|B01J-020/28/016|B01J-020/28/057|B01J-020/30/07|B01J-2220/4875|B02C-018/14|B07B-001/42|B65G-033/24|C01C-001/18/5|C01C-001/24|C01P-2004/60|C01P-2006/12|C02F-001/00/1|C02F-001/28/5|C02F-001/66|C02F-001/74|C02F-2101/30|C02F-2103/007|C02F-2303/04|C04B-018/14/6|C04B-028/04|C04B-2103/302|C05G-003/00|C05G-003/00/64|C05G-005/20|C09D-175/06|Y02A-050/2346|Y02A-050/2358|Y02C-010/04|Y02W-030/705 (GR1) C05D-001/00[RK1]; C05D-003/00[RK2]; C05D-005/00[RK3]; C05D-009/00[RK4]; C05D-009/02[RK5]; C05G-003/80[RK6] A01G-025/02|B01D-029/03|B01D-046/00/36|B01D-050/00/4|B01D-053/04|B01D-053/26|B01D-053/60|B01D-053/62|B01D-053/78|B01D-053/94/09|B01D-2251/50|B01D-2251/61|B01D-2257/504|B01D-2258/0283|B01D-2258/06|B01F-007/18|B01F-015/06/6|B01J-019/00/66|B01J-019/18|B01J-020/26/2|B01J-020/28/016|B01J-020/28/057|B01J-020/30/07|B01J-2220/4875|B02C-018/14|B07B-001/42|B65G-033/24|C01C-001/18/5|C01C-001/24|C01P-2004/60|C01P-2006/12|C02F-001/00/1|C02F-001/28/5|C02F-001/66|C02F-001/74|C02F-2101/30|C02F-2103/007|C02F-2303/04|C04B-018/14/6|C04B-028/04|C04B-2103/302|C05G-003/00|C05G-003/00/64|C05G-005/20|C09D-175/06|Y02A-050/2346|Y02A-050/2358|Y02C-010/04|Y02W-030/705 A01G-025/00|B01D-053/62|B01D-053/78|C02F-001/461|C02F-001/66|C05G-003/80 A01G-025/00|B01D-053/62|B01D-053/78|C02F-001/461|C02F-001/66|C05G-003/80 PENDING (CN121247965)|PENDING ALIVE (CN121247965)|ALIVE (CN121247965)|LEGAL DETAILS FOR CN121247965|Actual or expected expiration date=2045-08-19|Legal state=ALIVE|Status=PENDING|Event publication date=2025-08-19|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511161089|Application date=2025-08-19|Standardized application number=2025CN-1161089|Event publication date=2026-01-02|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121247965|Publication stage code=A|Publication date=2026-01-02|Standardized publication number=CN121247965|Event publication date=2026-01-02|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2026-01-20|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121247965)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKcWG9p3C3vb81fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080362160&ekey=2164&xpn=CN121247965&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=LgYKPURKoM4fAEXS%252FozvMpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121247965)|CN (CN121247965)|NAME=UNIV SOUTH SCIENCE & TECHNOLOGY CHINA , COUNTRY=CN (CN121247965)|NAME=FAN BING;JOHNSON IP , REG=44268 (CN121247965)|CN (CN121247965)|NAME=LEI YANG, COUNTRY=CN |NAME=PU YING 0 1 Titre: (CN121247965)|Improved agricultural irrigation water, application method thereof and method for simultaneously realizing preparation, carbon sequestration and mineral weathering acceleration of improved agricultural irrigation water Résumé: (CN121247965)|The invention discloses improved agricultural irrigation water, an application method thereof and a method for simultaneously realizing preparation, carbon sequestration and mineral weathering acceleration of the improved agricultural irrigation water, and relates to the technical field of agricultural irrigation and carbon sequestration. The method is based on an electrochemical treatment device, the electrochemical treatment device comprises an open reaction tank, an external power supply, an anode, a cathode and a barrier piece, the anode, the cathode and the barrier piece are arranged in the open reaction tank, and the area nearby the anode is used for being filled with minerals; the blocking piece is used for blocking minerals in an area near the anode; the method comprises the following steps: filling mineral into an area near an anode, introducing agricultural irrigation water into an open reaction tank, starting an external power supply for electrolysis, and simultaneously realizing preparation of improved agricultural irrigation water, carbon sequestration and mineral weathering acceleration. The improved agricultural irrigation water is used for agricultural irrigation, can neutralize acidified soil, supplement lost nutrients of the soil, provide required nutrient elements for plants, reduce application of chemical fertilizers and capture carbon dioxide, and has good agricultural benefits and environmental benefits. 2 Abstract gpt-4o-mini yes The article describes a method for accelerating mineral weathering and carbon sequestration using electrochemical treatment, which aligns with the topic of enhanced weathering and CO₂ capture.
2 CN202311752222 CN202311752222 CN117551832 108513206 CN117551832 A 2024-02-13 [CN117551832] 2023-12-19 2023-12-19 2024-02-13 (CN117551832)|2043-12-19 (CN117551832)|Iron-making device for reactive distillation, dealkalization, carbon sequestration and reduction of high-iron red mud (CN117551832)|The invention provides a reactive distillation dealkalization carbon sequestration and reduction ironmaking device for high-iron red mud. The reactive distillation dealkalization carbon sequestration and reduction ironmaking device mainly comprises reactive distillation dealkalization carbon sequestration equipment, fluidized reduction reaction magnetic separation equipment and Y-shaped entrained-flow bed gasifier in-situ reduction ironmaking equipment, the reactive distillation dealkalization and carbon sequestration equipment is of a cross-flow type tower plate structure, the number of tower plates is 1-30 layers of theoretical plates, the distance between the plates is 250-900 mm, a red mud slurry distributor is arranged at the top of the tower, a mixed flue gas distributor is arranged at the bottom of the tower, a purified flue gas outlet is formed in the top of the tower, and a dealkalization and carbon sequestration red mud outlet is formed in the bottom of the tower; in the fluidized drying-reduction reaction-magnetic separation equipment, a fluidized drying tower is a turbulent fluidized bed, a fluidized reduction reactor is a pulse riser crushing reactor, and a dry magnetic separator is used for magnetic separation; a cylindrical gasification section is arranged on the upper portion of the Y-shaped entrained-flow bed gasification reduction ironmaking furnace, a cylindrical settler separator is arranged on the lower portion of the Y-shaped entrained-flow bed gasification reduction ironmaking furnace, a top nozzle and a side nozzle are arranged on the top of the gasification section, the nozzles are distributed to be of an inverted-Y-shaped structure, and a slag outlet, a molten iron outlet and an emergency treatment opening are formed in the bottom of the settler separator. CHINA UNIVERSITY OF PETROLEUM EAST CHINA (CN117551832)|CHINA UNIVERSITY OF PETROLEUM (EAST CHINA) ([CN]) TIAN YUANYU|QIAO YINGYUN|TIAN YILIANG|ZHANG YANPENG|YE ZHIGANG (CN117551832)|TIAN YUANYU|QIAO YINGYUN|TIAN YILIANG|ZHANG YANPENG|YE ZHIGANG (CN117551832)|The high-value utilization of the high-iron red mud containing more than 30 iron oxides is difficult to solve, and the root causes are that the sodium oxide content in the high-iron red mud exceeds the standard and the non-magnetic iron oxide content is high.|The soluble alkali can be used at normal temperature and normal pressureCO ventilation 2 Or the alkali is removed by a water washing mode, but the part occupies smaller proportion, most of the alkali is insoluble alkali, particularly the sodium-silica slag in the Bayer process red mud occupies larger proportion, which occupies about 35 to 45 percent, and the removal of the alkali is one of the problems which are difficult to solve worldwide at present and is also a key problem affecting the further bulk utilization of the red mud.| (CN117551832)|1. The high-iron red mud reaction rectifying dealkalized carbon fixation and reduction iron making device is characterized by mainly comprising three working procedure devices of reaction rectifying dealkalized carbon fixation, fluidization reduction reaction magnetic separation and Y-type entrained flow gasifier in-situ reduction iron making; the bottom of the reaction rectifying tower is combined with the water washing desalting tower and the brine return line thereof through a filter press and a mixed slurry pump to form reaction rectifying dealkalization carbon fixing process equipment, the mass concentration of the high-iron red mud body treated by the reaction rectifying tower is 5-60%, and the spray density in the tower is 5-120m 3 /m 2 H, the flow velocity of the soft water in the countercurrent upward direction of the water washing desalting tower is 0.001-1.5m/s; the fluidization drying tower forms fluidization reduction reaction magnetic separation process equipment through a drying gas-solid separator at the top, a reduction tail gas pipeline at the bottom, a afterburner of the fluidization drying tower, a fluidization reduction reactor and a magnetic separation separator of the fluidization reduction reactor, wherein the fluidization drying temperature is 100-180 ℃, the reduction reaction temperature is 700-1300 ℃, and the purity of the magnetic separated fine iron ore powder is 40-95% (mass); the Y-type entrained-flow bed gasifying reduction iron-making furnace has cylindrical gasifying section in the upper part and cylindrical settler in the lower part, and top nozzle and side nozzle are set in the top of the gasifying sectionThe nozzles are distributed in an inverted Y-shaped structure, and a slag outlet, a tapping hole and an emergency treatment hole are arranged at the bottom of the settler separator; the reaction rectifying dealkalization carbon fixing process equipment is communicated with a fluidization drying tower of the fluidization reduction magnetic separation process equipment through a dehydration press filter at the bottom of the washing desalination tower, and the fluidization drying tower of the fluidization reduction magnetic separation process equipment is communicated with a flue gas distributor at the bottom of the washing desalination tower through a top drying gas-solid separator; the fluidized reduction reactor of the fluidized reduction magnetic separation process equipment is communicated with a feeding nozzle (a top nozzle and a side nozzle) of the Y-type entrained flow gasification reduction iron making furnace through a reduction reaction gas-solid separator, a cooler and a magnetic separation separator at the top, and a mixing bin of the fluidized reduction reaction magnetic separation process equipment is communicated with a fluidized gas feeding pipeline at the bottom of the fluidized reduction reactor of the fluidized reduction magnetic separation process equipment through an iron making tail gas outlet of a bottom sedimentation separator, so that a circulating system for rectifying, dealkalizing, carbon fixing and reduction iron making of the high-speed rail red mud is formed.| (CN117551832)|The invention provides a high-iron red mud reaction rectifying dealkalization carbon fixing and reduction iron making device, which mainly comprises reaction rectifying dealkalization carbon fixing equipment, fluidization reduction reaction magnetic separation equipment and Y-type entrained flow gasifier in-situ reduction iron making equipment; the reaction rectifying dealkalization carbon fixing equipment is of a through-flow type column plate structure, the number of column plates is 1-30 layers of theoretical plates, the plate spacing is 250-900mm, the top of the column is provided with a red mud distributor, the bottom of the column is provided with a mixed flue gas distributor, the top of the column is provided with a purified flue gas outlet, and the bottom of the column is provided with a dealkalization carbon fixing red mud outlet; in the fluidized drying-reduction reaction-magnetic separation equipment, a fluidized drying tower is a turbulent fluidized bed, a fluidized reduction reactor is a pulse riser crushing reactor, and a dry magnetic separator is used for magnetic separation; the upper part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical gasification section, the lower part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical settler separator, a top nozzle and a side nozzle are arranged at the top of the gasification section, the nozzles are distributed in an inverted Y-shaped structure, and a slag outlet, a molten iron outlet and an emergency treatment port are arranged at the bottom of the settler separator. The invention provides a high-iron red mud reaction rectifying dealkalization carbon fixation and reduction iron making device, belonging to the field of environmental protection.|the invention provides a high-iron red mud reaction rectifying dealkalization carbon fixation and reduction ironmaking device, which mainly comprises three working procedure devices of reaction rectifying dealkalization carbon fixation, fluidization reduction reaction magnetic separation and Y-type entrained flow gasifier in-situ reduction ironmaking; the bottom of the reaction rectifying tower is combined with the water washing desalting tower and the brine washing return line through a filter press and a mixed slurry pump to form reaction rectifying dealkalization carbon fixing process equipment, the concentration mass of the high-iron red mud body treated by the reaction rectifying tower is 5-60%, and the spray density in the tower is 5-120m 3 /m 2 H, the flow velocity of the soft water in the countercurrent upward direction of the water washing desalting tower is 0.001-1.5m/s; the fluidization drying tower forms fluidization reduction reaction magnetic separation process equipment through a drying gas-solid separator at the top, a reduction tail gas pipeline at the bottom, a afterburner of the fluidization drying tower, a fluidization reduction reactor and a magnetic separation separator of the fluidization reduction reactor, wherein the fluidization drying temperature is 100-180 ℃, the reduction reaction temperature is 700-1300 ℃, and the purity of the magnetic separated fine iron ore powder is 40-95%; the upper part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical gasification section, the lower part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical settler separator, a top nozzle and a side nozzle are arranged at the top of the gasification section, the nozzles are distributed in an inverted Y-shaped structure, and a slag outlet, a molten iron outlet and an emergency treatment port are arranged at the bottom of the settler separator; the reaction rectifying dealkalization carbon fixing process equipment is communicated with a fluidization drying tower of the fluidization reduction magnetic separation process equipment through a dehydration press filter at the bottom of the washing desalination tower, and the fluidization drying tower of the fluidization reduction magnetic separation process equipment is communicated with a flue gas distributor at the bottom of the washing desalination tower through a top drying gas-solid separator; the fluidized reduction reactor of the fluidized reduction reaction magnetic separation process equipment passes through a reduction reaction gas-solid separator, a cooler, a magnetic separation separator and a mixing bin and Y-shaped airflow at the topThe feeding nozzle (top nozzle and side nozzle) of the bed gasification reduction iron-making furnace is communicated, and the Y-shaped entrained flow gasification reduction iron-making furnace is communicated with a fluidization gas feeding pipeline at the bottom of a fluidization reduction reactor of the fluidization reduction reaction magnetic separation process equipment through an iron-making tail gas outlet of a bottom sedimentation separator, so that a circulation system for high-iron red mud reaction, rectification, dealkalization, carbon fixation and reduction iron-making is formed.| (CN117551832)|RED MUD(100,34)|CARBON FIXATION(100,21)|FLUIDIZATION DRYING TOWER(100,16)|REDUCTION IRON MAKING(100,14)|RED MUD REACTION(100,12)|REDUCTION(100,9)|DEALKALIZATION CARBON FIXATION(100,7)|DEALKALIZED CARBON FIXATION(100,3)|HIGHSPEED RAIL(100,2)|HIGHSPEED RAIL RED MUD(100,2)|WASHING DESALINIZATION TOWER(85,6)|GASIFYING SECTIONTHE NOZZLE(62,1)|FLUIDIZATION REDUCTION REACTOR(56,10)|DRYING TOWER(55,17)|SETTLER SEPARATOR(55,17)|DEALKALIZATION CARBON FIXING(50,6)|FLUIDIZATION REDUCTION(45,4)|REACTION RECTIFYING DEALKALIZATION(43,3)|FLUIDIZED REDUCTION REACTOR(41,10)|CYLINDRICAL SETTLER SEPARATOR(40,6)|PRESSURECO VENTILATION(38,1)|TOWER(35,40)|REDUCTION REACTOR(33,10)|FLUIDIZATION REDUCTION REACTION(30,8)|SLAG OUTLET(30,7)|MAGNETIC SEPARATION(29,36)|TURBULENT FLUIDIZED BED(29,7)|MOLTEN IRON OUTLET(29,3)|FINE IRON ORE POWDER(29,2)|GASIFYING SECTIONTHE NOZZLE TOP(29,1)|FLUE GAS DISTRIBUTOR(28,8)|RISER CONVEYING BED(28,6)|FLUIDIZATION DRYING TEMPERATURE(28,2)|FLUIDIZED GAS FEEDING PIPELINE(27,2)|RED MUD BULK UTILIZATION(27,1)|BOTTOM SEDIMENTATION SEPARATOR(26,3)|BED GASIFICATION REDUCTION(26,1)|CYLINDRICAL SETTLER(26,1)|MAGNETIC SEPARATION SEPARATOR(25,8)|RECTIFICATION(25,6)|SODIUM SILICA SLAG(25,1)|DEALKALIZATION(24,8)|FLUIDIZED REDUCTION(24,5)|FLUIDIZED DRYING TOWER(24,4)|BULK UTILIZATION(24,1)|REACTION RECTIFYING(24,1)|FLOW GASIFICATION REDUCTION(23,12)|IRON MAKING FURNACE(22,19)|SPRAY DENSITY(22,3)|BUBBLING FLUIDIZED BED(21,6)|DRY MAGNETIC SEPARATOR(21,1)|PULSE RISER(21,1)|MIXING BIN(20,7)|DEHYDRATION(20,3)|GAS SOLID SEPARATOR(19,11)|GASIFICATION REDUCTION(19,7)|AFTERBURNER(19,5)|FLUIDIZED REDUCTION MAGNETIC SEPARATION(19,4)|COUNTERCURRENT UPWARD DIRECTION(19,3)|GASIFIER(19,3)|REDUCTION TAIL GAS PIPELINE(19,3)|FEED NOZZLE(19,2)|GAS FEED(19,2)|PURITY(19,2)|FLUIDIZATION GAS(19,1)|RED MUD DISTRIBUTOR(18,2)|TAPPING HOLE(18,2)|DEALKALIZATION CARBON FIXING EQUIPMENT(18,1)|GASIFICATION SECTION(17,14)|EMERGENCY TREATMENT PORT(17,6)|INSOLUBLE BASE(17,2)|RECTIFYING(17,1)|CYLINDRICAL GASIFICATION SECTION(16,6)|FLUIDIZED REDUCTION REACTION(16,3)|PULSE RISER REACTOR(16,3)|DRYING TEMPERATURE(16,2)|CYLINDRICAL GASIFYING SECTION(16,1)|RED MUD OUTLET(16,1)|EMERGENCY TREATMENT(15,11)|TOP NOZZLE(15,10)|COOLER(15,4)|SOLUBLE ALKALI(15,2)|TOPTHE(15,1)|PACKED TOWER(14,3)|CIRCULATION(14,2)|MAGNETIC SEPARATION EQUIPMENT(14,2)|HOLLOW TOWER(14,1)|REDUCTION REACTION(13,14)|MIXED SLURRY PUMP(13,5)|DRYING GAS SOLID SEPARATOR(13,4)|FLUIDIZED DRYING REDUCTION REACTION(13,1)|PIPELINE(13,1)|GAS OUTLET(12,7)|EMERGENCY TREATMENT HOLE(12,5)|WATER COUNTERCURRENT UPWARD DIRECTION(12,3)|FLUE GAS(11,34)|IRON MAKING TAIL(11,6)|FLUE GAS OUTLET(11,4)|WATER WASHING(11,1)|NOZZLE SIDE(10,19)|REACTION BOTTOM(10,5)|SLAG HOLE(10,3)|IRON OXIDE(10,2)|CARBON FIXING EQUIPMENT(10,1)|ENVIRONMENTAL PROTECTION(10,1)|DOWNCOMER(9,2)|FLUE GAS TOWER(9,2)|PLATE SPACING(9,2)|RED MUD BODY DISTRIBUTOR(9,2)|IRON OXIDE CONTENT(9,1)|SODIUM OXIDE CONTENT(9,1)|COMBUSTION FLUE GAS(8,7)|INSOLUBLE ALKALINE SUBSTANCE(8,5)|OXYGEN CONTENT(8,3)|REDUCTION IRON MAKING FURNACE(8,3)|SPRAYING(8,3)|COLUMN PLATE(8,2)|REACTOR(8,2)|DRYING REDUCTION REACTION(8,1)|LARGE PROPORTION(8,1)|MASS CONCENTRATION(8,1)|SMALL PROPORTION(8,1)|Y SHAPED AIRFLOW(8,1)|FILTER PRESS(7,5)|OXIDANT(7,4)|EMPTYING(7,3)|REDUCTION REACTION TEMPERATURE(7,3)|SHUTDOWN(7,3)|TOWER PLATE(7,3)|CARBON FIXING(7,2)|FLOW VELOCITY(7,2)|HEAT INSULATING LINING(7,2)|REACTIVE RECTIFYING TOWER(7,2)|RED MUD BODY OUTLET(7,2)|BRINE WASHING RETURN LINE(7,1)|SOFT WATER(6,5)|ULTRALOW EMISSION(6,3)|VOLUME CONTENT(6,3)|WALL REFRACTORY LINING LAYER(6,3)|BAYER PROCESS RED MUD(6,1)|DEHYDRATED GAO TIECHI SLURRY(6,1)|REDUCTION IRON MAKING EQUIPMENT(6,1)|HIGH IRON RED MUD(5,11)|INVERTED Y SHAPED STRUCTURE(5,7)|OXYGEN ENRICHED AIR(5,3)|UPPER MIDDLE(5,3)|BRINE RETURN LINE(5,2)|FERROCOKE RESIDUE(5,2)|RED MUD DEALKALIZATION(5,2)|SODIUM OXIDE(5,2)|COLUMN PLATE STRUCTURE(5,1)|ROOT CAUSE(5,1)|WATER VAPOR(4,6)|DEALKALIZATION RATE(4,3)|RED MUD RESOURCE(4,3)|EMPTY TOWER(4,2)|BAYER(4,1)|CIRCULATION SYSTEM(4,1)|DEHYDRATING AGENT RED MUD DILUTION(4,1)|DESALINIZATION TOWER(4,1)|DURABLE DEALKALIZATION(4,1)|PARTSTHE CLOTH(4,1)|REACTION RECTIFICATION DEALKALIZATION(4,1)|SIPHON MOLTEN IRON OUTLET(4,1)|HORIZONTAL DIRECTION(3,3)|IRON ORE FINE POWDER(3,2)|RED MUD TON(3,2)|ALUMINUM COMPANY AMERICAN(3,1)|ALUMINUM ELECTROLYTE(3,1)|COMBUSTION SMOKE(3,1)|DEALKALIZING RED MUD(3,1)|DESALTED RED MUD(3,1)|FERROFERRIC OXIDE(3,1)|FINE IRON ORE PURITY(3,1)|FLUE GAS GRADING UTILIZATION(3,1)|FLUIDIZED DRYING TOWER GAS(3,1)|HOT MOLTEN IRON(3,1)|HYDRATED GARNET(3,1)|REACTIVE ACTIVITY GRADING(3,1)|REAGENT GRADE(3,1)|REFINED IRON ORE POWDER(3,1)|SLURRY BLOCKAGE(3,1)|SMOKE PURIFICATION(3,1)|SOLIDIFIED SLAG LAYER(3,1)|THICKENED RED MUD SLURRY(3,1)|UTILIZATION INDUSTRIAL CHAIN(3,1)|WEAK MAGNETISM(3,1)|YUAN TON IRON(3,1)|ALKALINE COMPONENT(2,2)|CANCRINITE(2,2)|DEHYDRATION FILTER PRESS(2,2)|ELECTROLYTIC ALUMINUM INDUSTRY(2,2)|PULVERIZED COAL(2,2)|REACTION ZONE(2,2)|TAIL GAS PIPELINE(2,2)|ACICULAR FERRIC OXIDE(2,1)|ALKALI SALT(2,1)| (CN117551832)|1. The high-iron red mud reaction rectifying dealkalized carbon fixation and reduction iron making device is characterized by mainly comprising three working procedure devices of reaction rectifying dealkalized carbon fixation, fluidization reduction reaction magnetic separation and Y-type entrained flow gasifier in-situ reduction iron making; the bottom of the reaction rectifying tower is combined with the water washing desalting tower and the brine return line thereof through a filter press and a mixed slurry pump to form reaction rectifying dealkalization carbon fixing process equipment, the mass concentration of the high-iron red mud body treated by the reaction rectifying tower is 5-60%, and the spray density in the tower is 5-120m 3 /m 2 H, the flow velocity of the soft water in the countercurrent upward direction of the water washing desalting tower is 0.001-1.5m/s; the fluidization drying tower forms fluidization reduction reaction magnetic separation process equipment through a drying gas-solid separator at the top, a reduction tail gas pipeline at the bottom, a afterburner of the fluidization drying tower, a fluidization reduction reactor and a magnetic separation separator of the fluidization reduction reactor, wherein the fluidization drying temperature is 100-180 ℃, the reduction reaction temperature is 700-1300 ℃, and the purity of the magnetic separated fine iron ore powder is 40-95% (mass); the Y-type entrained-flow bed gasifying reduction iron-making furnace has cylindrical gasifying section in the upper part and cylindrical settler in the lower part, and top nozzle and side nozzle are set in the top of the gasifying sectionThe nozzles are distributed in an inverted Y-shaped structure, and a slag outlet, a tapping hole and an emergency treatment hole are arranged at the bottom of the settler separator; the reaction rectifying dealkalization carbon fixing process equipment is communicated with a fluidization drying tower of the fluidization reduction magnetic separation process equipment through a dehydration press filter at the bottom of the washing desalination tower, and the fluidization drying tower of the fluidization reduction magnetic separation process equipment is communicated with a flue gas distributor at the bottom of the washing desalination tower through a top drying gas-solid separator; the fluidized reduction reactor of the fluidized reduction magnetic separation process equipment is communicated with a feeding nozzle (a top nozzle and a side nozzle) of the Y-type entrained flow gasification reduction iron making furnace through a reduction reaction gas-solid separator, a cooler and a magnetic separation separator at the top, and a mixing bin of the fluidized reduction reaction magnetic separation process equipment is communicated with a fluidized gas feeding pipeline at the bottom of the fluidized reduction reactor of the fluidized reduction magnetic separation process equipment through an iron making tail gas outlet of a bottom sedimentation separator, so that a circulating system for rectifying, dealkalizing, carbon fixing and reduction iron making of the high-speed rail red mud is formed.|2. The reaction, rectification, dealkalization, carbon fixation and reduction iron making device for the high-iron red mud according to claim 1 is characterized in that the reaction rectifying tower is of a flow-through structure without a downcomer, a high-iron red mud body distributor is arranged at the top of the tower, the plate spacing of the flow-through tower plates is 250-900mm, a mixed flue gas distributor is arranged at the bottom of the tower, a purified flue gas outlet is arranged at the top of the tower, and a dealkalized carbon fixation red mud body outlet is arranged at the bottom of the tower.|3. The high-iron red mud reaction, rectification, dealkalization, carbon fixation and reduction iron making device according to claim 1, which is characterized in that CO in combustion flue gas 2 The content is 12-25% of SO x The content is 0-50000PPm and NO x The content is 0-3000PPm, and the flow rate in the flue gas tower is 0.5-3.0m/s.|4. The high-iron red mud reaction, rectification, dealkalization, carbon fixation and reduction ironmaking device according to claim 1, which is characterized in that the water washing desalting tower is a flow-through plate tower, a packed tower or a hollow tower, the fluidization drying tower is a bubbling fluidized bed, a turbulent fluidized bed or a riser conveying bed, and the fluidization reduction reactor is a pulse riser reactor, a riser conveying bed, a bubbling fluidized bed or a turbulent fluidized bed.|5. The high-iron red mud reaction, rectification, dealkalization, carbon fixation and reduction iron making device according to claim 1, which is characterized in that the upper part of the Y-shaped entrained flow gasification reduction iron making furnace is a cylindrical gasification section, the lower part is a cylindrical settler separator, and the gasification section and the settler separator are in an inverted T-shaped structure; the gasification section adopts a water-cooled wall refractory lining layer, a lower spraying type top nozzle is arranged at the top, more than 3 side nozzles are arranged at the upper middle part along the circumference, and the nozzles are distributed in an inverted Y-shaped structure; the included angle between the side nozzle and the horizontal direction is-15 degrees to 15 degrees, and the included angle between the side nozzle and the radial direction is-5 degrees to 75 degrees; the separator of the settler adopts a heat-insulating lining, and the bottom of the separator is provided with a slag hole, a siphon type iron outlet and an emergency treatment hole; an emergency treatment port is arranged at the bottom of the separator of the settler to ensure emptying during shutdown or emergency.|6. The high-iron red mud reaction rectifying dealkalization carbon fixation and reduction ironmaking device according to claim 1, which is characterized in that the oxidant of the Y-type entrained flow gasification reduction ironmaking furnace is a mixture of water vapor and oxygen, air or oxygen-enriched air with the oxygen content of more than 21%, wherein the volume content of the water vapor is 0-40%. (CN117551832)|TECHNICAL FIELD|[0001] The invention provides a high-iron red mud reaction rectifying dealkalization carbon fixation and reduction iron making device, belonging to the field of environmental protection.|BACKGROUND ART|[0002] The red mud is pollution high alkali-containing waste residue discharged when alumina is extracted in the electrolytic aluminum industry, and 1.0-2.0 tons of red mud is additionally produced for each 1 ton of alumina generally. The recycling is an internationally recognized effective means for utilizing the red mud, and five utilization technologies of powder materials, element extraction, cementing materials, road materials and ceramic building materials are developed at home and abroad, but are all in the technical growth period at present and cannot be operated commercially.|[0003] The high-value utilization of the high-iron red mud containing more than 30 iron oxides is difficult to solve, and the root causes are that the sodium oxide content in the high-iron red mud exceeds the standard and the non-magnetic iron oxide content is high. The red mud is high-alkalinity solid waste, the pH value of the red mud is as high as 11-13, and alkaline substances in the red mud are mainly soluble alkali (free alkali) and insoluble alkali (combined alkali). The free alkali mainly comprises NaOH and Na 2 CO 3 、NaHCO 3、 NaAl(OH) 4 、Na 2 SiO 3 Etc., insoluble bases include calcite, cancrinite, hydrated garnet, sodalite and tricalcium aluminate, cancrinite being the main alkali-containing substance, sodium oxide (Na 2 O) is a major basic oxide with a content of up to 12.91% and is mainly present in the form of caustic soda, sodium aluminate and sodium aluminosilicate. The soluble alkali can be used at normal temperature and normal pressureCO ventilation 2 Or the alkali is removed by a water washing mode, but the part occupies smaller proportion, most of the alkali is insoluble alkali, particularly the sodium-silica slag in the Bayer process red mud occupies larger proportion, which occupies about 35 to 45 percent, and the removal of the alkali is one of the problems which are difficult to solve worldwide at present and is also a key problem affecting the further bulk utilization of the red mud. In addition, besides ferroferric oxide with strong magnetism, acicular ferric oxide, sodium ferrite and hydroxyl ferric oxide with non-magnetism or weak magnetism contained in the high-iron red mud directly influence the magnetic separation effect and recovery rate, and a high-efficiency, rapid and low-cost reduction magnetization technology and equipment thereof are needed.|[0004] The electrolytic aluminum is used as a large thermal power generation matched with the industries of high energy consumption and high pollution. CO in the flue gas 2 、SO x And NO x The acid gas is used for dealkalizing the red mud, so that the two problems of acid-base neutralization, waste treatment by waste, and meanwhile, the dealkalization of the red mud, flue gas decarburization and ultralow emission are effectively and low-cost solved. CO has been applied on a large scale by American aluminum company in West Australia 2 Dealkalization by gaseous and liquid CO 2 Added into the thickened red mud slurry, CO 2 The alkaline component in the slurry reacts with the alkaline component to achieve the purpose of dealkalization, but the dealkalization rate is less than 50% by adopting a gas dispersion method of introducing flue gas into red mud or a red mud spraying method at present. In addition, due to SO x Acid is stronger than CO 2 The method is easy to react with insoluble alkaline substances, can greatly improve the dealkalization rate, but the existing flue gas dealkalization process does not realize the grading utilization of flue gas, so that the insoluble alkaline substances become the durable and easy dealkalization of red mud. Therefore, research and development of high-iron red mud flue gas multiphase flow reaction rectification dealkalization carbon fixation and reduction iron-making technology and equipment thereof are needed, and SO is broken through x /CO 2 According to the industrial bottlenecks of high-efficiency utilization of reactive activity grading, slurry blockage, high-efficiency dispersion mass transfer, reaction and the like, a novel technology of a high-value utilization industrial chain of high-iron red mud resources is constructed, and a guarantee is provided for sustainable high-quality development of the electrolytic aluminum industry.|DISCLOSURE|3. Summary of the invention|[0005] The invention aims to overcome the defects of the existing high-iron red mud recycling technology, and provides a high-iron red mud reaction rectifying dealkalization carbon fixation and reduction iron-making device, which solves the problem of low-cost and high-efficiency removal of insoluble alkaline substances from red mud, and simultaneously solves the problem of high-value utilization of high-iron red mud resources by fluidized bed drying, reduction magnetization, magnetic separation and entrained flow in-situ reduction iron-making; in addition, the acid gas in the flue gas is effectively utilized according to the reactive grade, and the problems of decarbonization and ultralow emission of the combustion flue gas are solved with high efficiency and low cost.|[0006] The technical scheme of the invention is as follows:|[0007] the invention provides a high-iron red mud reaction rectifying dealkalization carbon fixation and reduction ironmaking device, which mainly comprises three working procedure devices of reaction rectifying dealkalization carbon fixation, fluidization reduction reaction magnetic separation and Y-type entrained flow gasifier in-situ reduction ironmaking; the bottom of the reaction rectifying tower is combined with the water washing desalting tower and the brine washing return line through a filter press and a mixed slurry pump to form reaction rectifying dealkalization carbon fixing process equipment, the concentration mass of the high-iron red mud body treated by the reaction rectifying tower is 5-60%, and the spray density in the tower is 5-120m 3 /m 2 H, the flow velocity of the soft water in the countercurrent upward direction of the water washing desalting tower is 0.001-1.5m/s; the fluidization drying tower forms fluidization reduction reaction magnetic separation process equipment through a drying gas-solid separator at the top, a reduction tail gas pipeline at the bottom, a afterburner of the fluidization drying tower, a fluidization reduction reactor and a magnetic separation separator of the fluidization reduction reactor, wherein the fluidization drying temperature is 100-180 ℃, the reduction reaction temperature is 700-1300 ℃, and the purity of the magnetic separated fine iron ore powder is 40-95%; the upper part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical gasification section, the lower part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical settler separator, a top nozzle and a side nozzle are arranged at the top of the gasification section, the nozzles are distributed in an inverted Y-shaped structure, and a slag outlet, a molten iron outlet and an emergency treatment port are arranged at the bottom of the settler separator; the reaction rectifying dealkalization carbon fixing process equipment is communicated with a fluidization drying tower of the fluidization reduction magnetic separation process equipment through a dehydration press filter at the bottom of the washing desalination tower, and the fluidization drying tower of the fluidization reduction magnetic separation process equipment is communicated with a flue gas distributor at the bottom of the washing desalination tower through a top drying gas-solid separator; the fluidized reduction reactor of the fluidized reduction reaction magnetic separation process equipment passes through a reduction reaction gas-solid separator, a cooler, a magnetic separation separator and a mixing bin and Y-shaped airflow at the topThe feeding nozzle (top nozzle and side nozzle) of the bed gasification reduction iron-making furnace is communicated, and the Y-shaped entrained flow gasification reduction iron-making furnace is communicated with a fluidization gas feeding pipeline at the bottom of a fluidization reduction reactor of the fluidization reduction reaction magnetic separation process equipment through an iron-making tail gas outlet of a bottom sedimentation separator, so that a circulation system for high-iron red mud reaction, rectification, dealkalization, carbon fixation and reduction iron-making is formed.|[0008] The reactive rectifying tower is of a through-flow type tower plate structure, the number of the tower plates is 1-30 layers of theoretical plates, the plate spacing is 250-900mm, the top of the tower is provided with a red mud distributor, the bottom of the tower is provided with a mixed flue gas distributor, the top of the tower is provided with a purified flue gas outlet, and the bottom of the tower is provided with a dealkalized carbon-fixing red mud outlet.|[0009] CO in combustion flue gas 2 The content is 12-25% of SO x The content is 0-50000PPm and NO x The content is 0-3000PPm, and the flow rate in the flue gas tower is 0.5-3.0m/s.|[0010] The water washing desalting tower is a flow-through plate tower, a packed tower or an empty tower.|[0011] The fluidized drying tower is a bubbling fluidized bed, a turbulent fluidized bed or a riser conveying bed, and the fluidized reduction reactor is a pulse riser reactor, a riser conveying bed, a bubbling fluidized bed or a turbulent fluidized bed.|[0012] The upper part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical gasification section, the lower part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical settler separator, and the gasification section and the settler separator are in an inverted T-shaped structure; the gasification section adopts a water-cooled wall refractory lining layer, a lower spraying type top nozzle is arranged at the top, more than 3 side nozzles are arranged at the upper middle part along the circumference, and the nozzles are distributed in an inverted Y-shaped structure; the included angle between the side nozzle and the horizontal direction is-15 degrees to 15 degrees, and the included angle between the side nozzle and the radial direction is-5 degrees to 75 degrees; the separator of the settler adopts a heat-insulating lining, and the bottom of the separator is provided with a slag hole, a siphon type iron outlet and an emergency treatment hole; an emergency treatment port is arranged at the bottom of the separator of the settler to ensure emptying during shutdown or emergency.|[0013] The oxidant of the Y-type entrained flow gasification reduction iron-making furnace is a mixture of water vapor and oxygen, air or oxygen-enriched air with the oxygen content of more than 21%, wherein the volume content of the water vapor is 0-40%.|[0014] The present invention will be described in detail with reference to examples.|DRAWINGS DESCRIPTION|4. Description of the drawings|[0015] The attached drawings are schematic diagrams of the present invention. The drawings of the drawings are as follows:|[0016] 1. the device comprises a slurry pump 2, a flue gas distributor 3, a reaction rectifying tower 4, a filter press 5, a mixed slurry pump 6, a washing desalting tower 7, a soft water distributor 8, a dehydration filter press 9, a afterburner 10, a fluidization drying tower 11, a dry gas-solid separator 12, a fluidization reduction reactor 13, a reduction reaction gas-solid separator 14, a cooler 15, a magnetic separation separator 16, a mixing bin 17, a Y-type entrained flow gasification reduction iron-making furnace 18, a settler separator 19, a top nozzle 20, a side nozzle 21, an iron-making tail gas outlet 22, an iron outlet 23, a slag hole 24 and an emergency treatment hole.|[0017] A. Purifying smoke B, salt water C, magnetic separation residue D, high-iron red mud E, combustion smoke F, soft water G, coal dust H and air|[0018] The process features of the present invention are described in detail below with reference to the accompanying drawings and examples.|INVENTION MODE|5. Detailed description of the preferred embodiments|[0019] The device mainly comprises three working procedures of reaction, rectification, dealkalization, carbon fixation, fluidized reduction, magnetic separation and in-situ reduction and iron making of a Y-type entrained flow gasifier; the bottom of the reaction rectifying tower (3) and the washing desalting tower (6) and a brine return line thereof form reaction rectifying dealkalization carbon fixing process equipment through a filter press (4) and a mixed slurry pump (5), the concentration mass of the high-iron red mud body treated by the reaction rectifying tower (3) is 5-60%, and the spray density in the tower is 5-120m 3 /m 2 H, the flow rate of the soft water in the countercurrent upward direction of the water washing desalination tower (5) is 0.001-1.5m/s; the fluidized drying tower (10) forms fluidized reduction reaction magnetic separation process equipment with a fluidized drying temperature of 100-180 ℃, a reduction reaction temperature of 700-1300 ℃ and a purity of the fine iron ore powder subjected to magnetic separation of 40-95% through a drying gas-solid separator (11) at the top, a reduction tail gas pipeline at the bottom, a afterburner (9) of the tail gas pipeline, a fluidized reduction reactor (12) and a magnetic separation separator (15) of the tail gas pipeline; the Y-type entrained-flow bed gasifying reduction ironmaking furnace (17) has a cylindrical gasification section at the upper part and a cylindrical settler separator (18) at the lower part, and a top nozzle (19) and a side nozzle (20) are arranged at the top of the gasification section, and the nozzles are divided into two partsThe cloth is of an inverted Y-shaped structure, and a slag outlet (23), a tapping hole (22) and an emergency treatment hole (24) are arranged at the bottom of the settler separator (18); the reaction rectifying dealkalization carbon fixation process equipment is communicated with a fluidization drying tower (10) of the fluidization reduction reaction magnetic separation process equipment through a dehydration filter press (8) at the bottom of the washing desalination tower (6), and the fluidization drying tower (10) of the fluidization reduction reaction magnetic separation process equipment is communicated with a flue gas distributor (2) at the bottom of the washing desalination tower (6) through a top drying gas-solid separator (11); the fluidized reduction reactor (12) of the fluidized reduction magnetic separation process equipment is communicated with a feeding nozzle (a top nozzle (19) and a side nozzle (20)) of the Y-type entrained-flow gasification reduction iron-making furnace (17) through a reduction reaction gas-solid separator (13), a cooler (14) and a magnetic separation separator (15) at the top and a mixing bin (16) thereof, and the Y-type entrained-flow gasification reduction iron-making furnace (17) is communicated with a fluidized gas feeding pipeline at the bottom of the fluidized reduction reactor (12) of the fluidized reduction magnetic separation process equipment through an iron-making tail gas outlet (21) of a bottom sedimentation separator (18), so that a circulating system for high-iron red mud reaction rectification dealkalization carbon fixation and reduction iron making is formed.|[0020] The reaction rectifying tower (3) is of a flow-through structure without a downcomer, the top of the tower is provided with a red mud body distributor, the plate spacing of the flow-through tower plates is 250-900mm, the bottom of the tower is provided with a combustion flue gas distributor (2), the top of the tower is provided with a flue gas outlet, and the bottom of the tower is provided with a red mud body outlet. CO in combustion flue gas 2 The content is 12-25% of SO x The content is 0-50000PPm and NO x The content is 0-3000PPm, and the flow rate of the flue gas in the reactive rectifying tower (3) is 0.5-3.0m/s.|[0021] The water washing desalting tower (6) is a flow-through plate tower, a packed tower or an empty tower, the fluidization drying tower (10) is a bubbling fluidized bed, a turbulent fluidized bed or a riser conveying bed, and the fluidization reduction reactor (12) is a pulse riser reactor, a riser conveying bed, a bubbling fluidized bed or a turbulent fluidized bed.|[0022] The upper part of the Y-shaped entrained flow gasification reduction iron-making furnace (17) is a cylindrical gasification section, the lower part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical settler separator (18), and the gasification section and the settler separator (18) are in an inverted T-shaped structure; the gasification section adopts a water-cooled wall refractory lining layer, a lower spraying type top nozzle (19) is arranged at the top, more than 3 side nozzles (20) are circumferentially arranged at the upper middle part, and the nozzles are distributed in an inverted Y-shaped structure; the included angle between the side nozzle and the horizontal direction is-15 degrees to 15 degrees, and the included angle between the side nozzle and the radial direction is-5 degrees to 75 degrees; the settler separator (18) adopts a heat insulation lining, and the bottom is provided with a slag outlet (23), a siphon type iron outlet (22) and an emergency treatment port (24); an ironmaking tail gas outlet (21) is arranged on the side surface of the top, and an emergency treatment port (24) is arranged at the bottom of the separator of the settler, so that emptying is ensured during shutdown or emergency.|[0023] The oxidant of the Y-type entrained flow gasification reduction iron-making furnace (17) is a mixture of water vapor and oxygen, air or oxygen-enriched air with the oxygen content of more than 21%, wherein the volume content of the water vapor is 0-40%.|[0024] In the concrete operation, the high-iron red mud D with the temperature of 10-100 ℃ is sent to the top of a reaction rectifying tower (3) through a slurry pump (1), and is in countercurrent contact with mixed flue gas with the temperature of 30-180 ℃ which is introduced from a flue gas distributor (2) at the bottom of the tower and passes through a flow-through column plate or a filler of 1-30 theoretical plates, wherein the feeding amount ratio of the mixed flue gas to red mud is 500-3000:1 (volume ratio); medium CO in flue gas in reactive distillation column (3) 2 The SOx and NOx acid gas and NaO, KO and alkaline salt thereof in the slurry are subjected to high-efficiency reactive distillation, SOx and NOx mainly react with insoluble alkaline substances at the lower part of the tower, and CO 2 The method mainly comprises the steps of reacting with soluble alkaline substances at the upper part of a tower, reducing the pH value of red mud slurry to be not more than 8 from 11-14, discharging purified flue gas A from the top of a reaction rectifying tower (3), discharging high-iron red mud slurry subjected to dealkalization and carbon fixation from the bottom of the reaction rectifying tower (3), and removing strong brine through a filter press (4); the dehydrated Gao Tiechi slurry is diluted by part of brine B, pumped to the top of a water washing desalting tower (6) through a mixed slurry pump (5), and is subjected to countercurrent water washing desalting with soft water introduced by a soft water distributor (7), and the part of brine B flowing out of the top of the water washing desalting tower (6) is used for diluting the dehydrated red mud, and part of brine B is mixed with strong brine and returned to an alumina extraction section; the desalted red mud flowing out of the bottom of the water washing desalting tower (6) is dehydrated by a dehydration press filter (8) and then is sent to a fluidization drying tower (10), the reduction tail gas is post-combusted in an afterburner (9) through air H and then is also sent to the bottom of the fluidization drying tower (10) for fluidization heating and drying, and the drying tail gas obtained by separating the drying gas-solid separator (11) at the top of the fluidization drying tower (10) is mixed with combustion flue gas E and then is sent to the bottom of the reaction rectifying tower (3); fluidized drying tower(10) The dry desalted high-iron red mud obtained by gas-solid separation at the top of the tower is sent into a fluidized reduction reactor (12) to carry out reduction magnetization reaction with the reduction ironmaking tail gas at 1300-1700 ℃, the reduction tail gas obtained by gas-solid separation of the reduction reaction at the top of the fluidized reduction reactor (12) is used as the fluidized drying gas of a fluidized drying tower (10) after being post-combusted, and the reduced red mud cooler (14) obtained by gas-solid separation at the top of the reduction fluidization reactor (13) is cooled and then subjected to magnetic separation by a magnetic separation separator (15) to recover fine iron ore powder; the refined iron ore powder and the pulverized coal are mixed in a mixing bin (16) and then sent into a Y-shaped entrained flow gasification reduction iron making furnace (17) by using an oxidant, in-situ gasification reduction iron making is carried out at 1300-1700 ℃, high-temperature molten iron, slag and reduction iron making tail gas downwards flow into a settler separator (18) at the bottom of the Y-shaped entrained flow gasification reduction iron making furnace (17), molten iron is obtained from an iron outlet (22) after sedimentation and layering, slag is obtained from a slag outlet (23) and iron making tail gas is sent from an iron making tail gas outlet (21), the iron making tail gas is sent back to a fluidization reduction reactor (12), and the molten iron and slag are discharged outwards as products.|[0025] The Y-type entrained-flow bed gasifying reduction iron-making furnace (17) is operated by fine iron ore powder and pulverized coal according to the proportion of C to Fe 2 O 3 The ratio is 1:1.1 to 4.0 are evenly mixed and sent into a mixing bin (16); the iron coal powder mixture and gasifying agent from the mixing bin (16) are sprayed into a gasification section through a top nozzle (19) and a radial inclined side nozzle (20) of a Y-type entrained-flow bed gasifying reduction iron-making furnace (17), and are gasified and reduced at the temperature of 1300-1700 ℃; the top nozzle (19) and the side nozzle (20) generate a plurality of jet flows which collide with each other in the center of the hearth to form a Y-shaped rotary impact high-temperature reaction zone, the Y-shaped rotary impact high-temperature reaction zone ignites each other to strengthen gasification reduction reaction, ferrocoke residues are thrown to the furnace wall of the gasification section, the rotational flow is downward, the retention and reaction time of the ferrocoke residues in the gasification section is prolonged by more than 20 times, and a solidified slag layer is formed on the surface of a refractory layer of a water-cooled wall of the gasification section to realize slag resistance; the iron-making tail gas, high-temperature molten iron and slag flow to a settler separator (18) through a discharge port in the center of a conical end socket of the gasification section, residual iron ore powder and carbon powder are subjected to thermal insulation for further reduction reaction, and the iron-making tail gas at 1300-1700 ℃ is discharged from an iron-making tail gas outlet (21) on the side surface of the top of the settler separator (18) and pumped into a fluidization reduction reactor (12) for reduction magnetization of high-iron red mud; high heightAfter the hot molten iron and the slag are settled and separated, the slag is discharged through a slag outlet, and the high-temperature molten iron is discharged through a siphon type molten iron outlet (22) and can maintain a stable molten iron-slag interface height.|[0026] The high-iron red mud reaction rectifying dealkalization carbon fixation and reduction ironmaking device provided by the invention realizes the graded utilization of acid gas in flue gas according to the reaction activity by the reaction rectifying tower, efficiently breaks through combustion flue gas decarburization and ultralow emission at low cost, solves the problem of low-cost and high-efficiency removal of insoluble alkaline substances by the high-iron red mud, improves the dealkalization rate from 50% to 98% in general, and ensures that the carbon fixation amount is less than 40KgCO 2 Per ton of 30% red mud is increased to 150KgCO 2 Per ton of red mud above 30%; the dealkalized and carbon-fixed high-iron red mud is subjected to reduction, magnetic separation and in-situ reduction and ironmaking by using the ironmaking tail gas, the purity of iron ore powder is improved by more than 30%, the iron recovery rate is improved by more than 99%, the ironmaking energy consumption is reduced by more than 50%, the cost is reduced by 500-1000 yuan/ton iron, and conditions are created for the high-value utilization of high-iron red mud resources. (CN117551832)|TECHNICAL FIELD|[0001] The invention provides a high-iron red mud reaction rectifying dealkalization carbon fixation and reduction iron making device, belonging to the field of environmental protection.|BACKGROUND ART|[0002] The red mud is pollution high alkali-containing waste residue discharged when alumina is extracted in the electrolytic aluminum industry, and 1.0-2.0 tons of red mud is additionally produced for each 1 ton of alumina generally. The recycling is an internationally recognized effective means for utilizing the red mud, and five utilization technologies of powder materials, element extraction, cementing materials, road materials and ceramic building materials are developed at home and abroad, but are all in the technical growth period at present and cannot be operated commercially.|[0003] The high-value utilization of the high-iron red mud containing more than 30 iron oxides is difficult to solve, and the root causes are that the sodium oxide content in the high-iron red mud exceeds the standard and the non-magnetic iron oxide content is high. The red mud is high-alkalinity solid waste, the pH value of the red mud is as high as 11-13, and alkaline substances in the red mud are mainly soluble alkali (free alkali) and insoluble alkali (combined alkali). The free alkali mainly comprises NaOH and Na 2 CO 3 、NaHCO 3、 NaAl(OH) 4 、Na 2 SiO 3 Etc., insoluble bases include calcite, cancrinite, hydrated garnet, sodalite and tricalcium aluminate, cancrinite being the main alkali-containing substance, sodium oxide (Na 2 O) is a major basic oxide with a content of up to 12.91% and is mainly present in the form of caustic soda, sodium aluminate and sodium aluminosilicate. The soluble alkali can be used at normal temperature and normal pressureCO ventilation 2 Or the alkali is removed by a water washing mode, but the part occupies smaller proportion, most of the alkali is insoluble alkali, particularly the sodium-silica slag in the Bayer process red mud occupies larger proportion, which occupies about 35 to 45 percent, and the removal of the alkali is one of the problems which are difficult to solve worldwide at present and is also a key problem affecting the further bulk utilization of the red mud. In addition, besides ferroferric oxide with strong magnetism, acicular ferric oxide, sodium ferrite and hydroxyl ferric oxide with non-magnetism or weak magnetism contained in the high-iron red mud directly influence the magnetic separation effect and recovery rate, and a high-efficiency, rapid and low-cost reduction magnetization technology and equipment thereof are needed.|[0004] The electrolytic aluminum is used as a large thermal power generation matched with the industries of high energy consumption and high pollution. CO in the flue gas 2 、SO x And NO x The acid gas is used for dealkalizing the red mud, so that the two problems of acid-base neutralization, waste treatment by waste, and meanwhile, the dealkalization of the red mud, flue gas decarburization and ultralow emission are effectively and low-cost solved. CO has been applied on a large scale by American aluminum company in West Australia 2 Dealkalization by gaseous and liquid CO 2 Added into the thickened red mud slurry, CO 2 The alkaline component in the slurry reacts with the alkaline component to achieve the purpose of dealkalization, but the dealkalization rate is less than 50% by adopting a gas dispersion method of introducing flue gas into red mud or a red mud spraying method at present. In addition, due to SO x Acid is stronger than CO 2 The method is easy to react with insoluble alkaline substances, can greatly improve the dealkalization rate, but the existing flue gas dealkalization process does not realize the grading utilization of flue gas, so that the insoluble alkaline substances become the durable and easy dealkalization of red mud. Therefore, research and development of high-iron red mud flue gas multiphase flow reaction rectification dealkalization carbon fixation and reduction iron-making technology and equipment thereof are needed, and SO is broken through x /CO 2 According to the industrial bottlenecks of high-efficiency utilization of reactive activity grading, slurry blockage, high-efficiency dispersion mass transfer, reaction and the like, a novel technology of a high-value utilization industrial chain of high-iron red mud resources is constructed, and a guarantee is provided for sustainable high-quality development of the electrolytic aluminum industry.|DISCLOSURE|3. Summary of the invention|[0005] The invention aims to overcome the defects of the existing high-iron red mud recycling technology, and provides a high-iron red mud reaction rectifying dealkalization carbon fixation and reduction iron-making device, which solves the problem of low-cost and high-efficiency removal of insoluble alkaline substances from red mud, and simultaneously solves the problem of high-value utilization of high-iron red mud resources by fluidized bed drying, reduction magnetization, magnetic separation and entrained flow in-situ reduction iron-making; in addition, the acid gas in the flue gas is effectively utilized according to the reactive grade, and the problems of decarbonization and ultralow emission of the combustion flue gas are solved with high efficiency and low cost.|[0006] The technical scheme of the invention is as follows:|[0007] the invention provides a high-iron red mud reaction rectifying dealkalization carbon fixation and reduction ironmaking device, which mainly comprises three working procedure devices of reaction rectifying dealkalization carbon fixation, fluidization reduction reaction magnetic separation and Y-type entrained flow gasifier in-situ reduction ironmaking; the bottom of the reaction rectifying tower is combined with the water washing desalting tower and the brine washing return line through a filter press and a mixed slurry pump to form reaction rectifying dealkalization carbon fixing process equipment, the concentration mass of the high-iron red mud body treated by the reaction rectifying tower is 5-60%, and the spray density in the tower is 5-120m 3 /m 2 H, the flow velocity of the soft water in the countercurrent upward direction of the water washing desalting tower is 0.001-1.5m/s; the fluidization drying tower forms fluidization reduction reaction magnetic separation process equipment through a drying gas-solid separator at the top, a reduction tail gas pipeline at the bottom, a afterburner of the fluidization drying tower, a fluidization reduction reactor and a magnetic separation separator of the fluidization reduction reactor, wherein the fluidization drying temperature is 100-180 ℃, the reduction reaction temperature is 700-1300 ℃, and the purity of the magnetic separated fine iron ore powder is 40-95%; the upper part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical gasification section, the lower part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical settler separator, a top nozzle and a side nozzle are arranged at the top of the gasification section, the nozzles are distributed in an inverted Y-shaped structure, and a slag outlet, a molten iron outlet and an emergency treatment port are arranged at the bottom of the settler separator; the reaction rectifying dealkalization carbon fixing process equipment is communicated with a fluidization drying tower of the fluidization reduction magnetic separation process equipment through a dehydration press filter at the bottom of the washing desalination tower, and the fluidization drying tower of the fluidization reduction magnetic separation process equipment is communicated with a flue gas distributor at the bottom of the washing desalination tower through a top drying gas-solid separator; the fluidized reduction reactor of the fluidized reduction reaction magnetic separation process equipment passes through a reduction reaction gas-solid separator, a cooler, a magnetic separation separator and a mixing bin and Y-shaped airflow at the topThe feeding nozzle (top nozzle and side nozzle) of the bed gasification reduction iron-making furnace is communicated, and the Y-shaped entrained flow gasification reduction iron-making furnace is communicated with a fluidization gas feeding pipeline at the bottom of a fluidization reduction reactor of the fluidization reduction reaction magnetic separation process equipment through an iron-making tail gas outlet of a bottom sedimentation separator, so that a circulation system for high-iron red mud reaction, rectification, dealkalization, carbon fixation and reduction iron-making is formed.|[0008] The reactive rectifying tower is of a through-flow type tower plate structure, the number of the tower plates is 1-30 layers of theoretical plates, the plate spacing is 250-900mm, the top of the tower is provided with a red mud distributor, the bottom of the tower is provided with a mixed flue gas distributor, the top of the tower is provided with a purified flue gas outlet, and the bottom of the tower is provided with a dealkalized carbon-fixing red mud outlet.|[0009] CO in combustion flue gas 2 The content is 12-25% of SO x The content is 0-50000PPm and NO x The content is 0-3000PPm, and the flow rate in the flue gas tower is 0.5-3.0m/s.|[0010] The water washing desalting tower is a flow-through plate tower, a packed tower or an empty tower.|[0011] The fluidized drying tower is a bubbling fluidized bed, a turbulent fluidized bed or a riser conveying bed, and the fluidized reduction reactor is a pulse riser reactor, a riser conveying bed, a bubbling fluidized bed or a turbulent fluidized bed.|[0012] The upper part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical gasification section, the lower part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical settler separator, and the gasification section and the settler separator are in an inverted T-shaped structure; the gasification section adopts a water-cooled wall refractory lining layer, a lower spraying type top nozzle is arranged at the top, more than 3 side nozzles are arranged at the upper middle part along the circumference, and the nozzles are distributed in an inverted Y-shaped structure; the included angle between the side nozzle and the horizontal direction is-15 degrees to 15 degrees, and the included angle between the side nozzle and the radial direction is-5 degrees to 75 degrees; the separator of the settler adopts a heat-insulating lining, and the bottom of the separator is provided with a slag hole, a siphon type iron outlet and an emergency treatment hole; an emergency treatment port is arranged at the bottom of the separator of the settler to ensure emptying during shutdown or emergency.|[0013] The oxidant of the Y-type entrained flow gasification reduction iron-making furnace is a mixture of water vapor and oxygen, air or oxygen-enriched air with the oxygen content of more than 21%, wherein the volume content of the water vapor is 0-40%.|[0014] The present invention will be described in detail with reference to examples.|DRAWINGS DESCRIPTION|4. Description of the drawings|[0015] The attached drawings are schematic diagrams of the present invention. The drawings of the drawings are as follows:|[0016] 1. the device comprises a slurry pump 2, a flue gas distributor 3, a reaction rectifying tower 4, a filter press 5, a mixed slurry pump 6, a washing desalting tower 7, a soft water distributor 8, a dehydration filter press 9, a afterburner 10, a fluidization drying tower 11, a dry gas-solid separator 12, a fluidization reduction reactor 13, a reduction reaction gas-solid separator 14, a cooler 15, a magnetic separation separator 16, a mixing bin 17, a Y-type entrained flow gasification reduction iron-making furnace 18, a settler separator 19, a top nozzle 20, a side nozzle 21, an iron-making tail gas outlet 22, an iron outlet 23, a slag hole 24 and an emergency treatment hole.|[0017] A. Purifying smoke B, salt water C, magnetic separation residue D, high-iron red mud E, combustion smoke F, soft water G, coal dust H and air|[0018] The process features of the present invention are described in detail below with reference to the accompanying drawings and examples.|INVENTION MODE|5. Detailed description of the preferred embodiments|[0019] The device mainly comprises three working procedures of reaction, rectification, dealkalization, carbon fixation, fluidized reduction, magnetic separation and in-situ reduction and iron making of a Y-type entrained flow gasifier; the bottom of the reaction rectifying tower (3) and the washing desalting tower (6) and a brine return line thereof form reaction rectifying dealkalization carbon fixing process equipment through a filter press (4) and a mixed slurry pump (5), the concentration mass of the high-iron red mud body treated by the reaction rectifying tower (3) is 5-60%, and the spray density in the tower is 5-120m 3 /m 2 H, the flow rate of the soft water in the countercurrent upward direction of the water washing desalination tower (5) is 0.001-1.5m/s; the fluidized drying tower (10) forms fluidized reduction reaction magnetic separation process equipment with a fluidized drying temperature of 100-180 ℃, a reduction reaction temperature of 700-1300 ℃ and a purity of the fine iron ore powder subjected to magnetic separation of 40-95% through a drying gas-solid separator (11) at the top, a reduction tail gas pipeline at the bottom, a afterburner (9) of the tail gas pipeline, a fluidized reduction reactor (12) and a magnetic separation separator (15) of the tail gas pipeline; the Y-type entrained-flow bed gasifying reduction ironmaking furnace (17) has a cylindrical gasification section at the upper part and a cylindrical settler separator (18) at the lower part, and a top nozzle (19) and a side nozzle (20) are arranged at the top of the gasification section, and the nozzles are divided into two partsThe cloth is of an inverted Y-shaped structure, and a slag outlet (23), a tapping hole (22) and an emergency treatment hole (24) are arranged at the bottom of the settler separator (18); the reaction rectifying dealkalization carbon fixation process equipment is communicated with a fluidization drying tower (10) of the fluidization reduction reaction magnetic separation process equipment through a dehydration filter press (8) at the bottom of the washing desalination tower (6), and the fluidization drying tower (10) of the fluidization reduction reaction magnetic separation process equipment is communicated with a flue gas distributor (2) at the bottom of the washing desalination tower (6) through a top drying gas-solid separator (11); the fluidized reduction reactor (12) of the fluidized reduction magnetic separation process equipment is communicated with a feeding nozzle (a top nozzle (19) and a side nozzle (20)) of the Y-type entrained-flow gasification reduction iron-making furnace (17) through a reduction reaction gas-solid separator (13), a cooler (14) and a magnetic separation separator (15) at the top and a mixing bin (16) thereof, and the Y-type entrained-flow gasification reduction iron-making furnace (17) is communicated with a fluidized gas feeding pipeline at the bottom of the fluidized reduction reactor (12) of the fluidized reduction magnetic separation process equipment through an iron-making tail gas outlet (21) of a bottom sedimentation separator (18), so that a circulating system for high-iron red mud reaction rectification dealkalization carbon fixation and reduction iron making is formed.|[0020] The reaction rectifying tower (3) is of a flow-through structure without a downcomer, the top of the tower is provided with a red mud body distributor, the plate spacing of the flow-through tower plates is 250-900mm, the bottom of the tower is provided with a combustion flue gas distributor (2), the top of the tower is provided with a flue gas outlet, and the bottom of the tower is provided with a red mud body outlet. CO in combustion flue gas 2 The content is 12-25% of SO x The content is 0-50000PPm and NO x The content is 0-3000PPm, and the flow rate of the flue gas in the reactive rectifying tower (3) is 0.5-3.0m/s.|[0021] The water washing desalting tower (6) is a flow-through plate tower, a packed tower or an empty tower, the fluidization drying tower (10) is a bubbling fluidized bed, a turbulent fluidized bed or a riser conveying bed, and the fluidization reduction reactor (12) is a pulse riser reactor, a riser conveying bed, a bubbling fluidized bed or a turbulent fluidized bed.|[0022] The upper part of the Y-shaped entrained flow gasification reduction iron-making furnace (17) is a cylindrical gasification section, the lower part of the Y-shaped entrained flow gasification reduction iron-making furnace is a cylindrical settler separator (18), and the gasification section and the settler separator (18) are in an inverted T-shaped structure; the gasification section adopts a water-cooled wall refractory lining layer, a lower spraying type top nozzle (19) is arranged at the top, more than 3 side nozzles (20) are circumferentially arranged at the upper middle part, and the nozzles are distributed in an inverted Y-shaped structure; the included angle between the side nozzle and the horizontal direction is-15 degrees to 15 degrees, and the included angle between the side nozzle and the radial direction is-5 degrees to 75 degrees; the settler separator (18) adopts a heat insulation lining, and the bottom is provided with a slag outlet (23), a siphon type iron outlet (22) and an emergency treatment port (24); an ironmaking tail gas outlet (21) is arranged on the side surface of the top, and an emergency treatment port (24) is arranged at the bottom of the separator of the settler, so that emptying is ensured during shutdown or emergency.|[0023] The oxidant of the Y-type entrained flow gasification reduction iron-making furnace (17) is a mixture of water vapor and oxygen, air or oxygen-enriched air with the oxygen content of more than 21%, wherein the volume content of the water vapor is 0-40%.|[0024] In the concrete operation, the high-iron red mud D with the temperature of 10-100 ℃ is sent to the top of a reaction rectifying tower (3) through a slurry pump (1), and is in countercurrent contact with mixed flue gas with the temperature of 30-180 ℃ which is introduced from a flue gas distributor (2) at the bottom of the tower and passes through a flow-through column plate or a filler of 1-30 theoretical plates, wherein the feeding amount ratio of the mixed flue gas to red mud is 500-3000:1 (volume ratio); medium CO in flue gas in reactive distillation column (3) 2 The SOx and NOx acid gas and NaO, KO and alkaline salt thereof in the slurry are subjected to high-efficiency reactive distillation, SOx and NOx mainly react with insoluble alkaline substances at the lower part of the tower, and CO 2 The method mainly comprises the steps of reacting with soluble alkaline substances at the upper part of a tower, reducing the pH value of red mud slurry to be not more than 8 from 11-14, discharging purified flue gas A from the top of a reaction rectifying tower (3), discharging high-iron red mud slurry subjected to dealkalization and carbon fixation from the bottom of the reaction rectifying tower (3), and removing strong brine through a filter press (4); the dehydrated Gao Tiechi slurry is diluted by part of brine B, pumped to the top of a water washing desalting tower (6) through a mixed slurry pump (5), and is subjected to countercurrent water washing desalting with soft water introduced by a soft water distributor (7), and the part of brine B flowing out of the top of the water washing desalting tower (6) is used for diluting the dehydrated red mud, and part of brine B is mixed with strong brine and returned to an alumina extraction section; the desalted red mud flowing out of the bottom of the water washing desalting tower (6) is dehydrated by a dehydration press filter (8) and then is sent to a fluidization drying tower (10), the reduction tail gas is post-combusted in an afterburner (9) through air H and then is also sent to the bottom of the fluidization drying tower (10) for fluidization heating and drying, and the drying tail gas obtained by separating the drying gas-solid separator (11) at the top of the fluidization drying tower (10) is mixed with combustion flue gas E and then is sent to the bottom of the reaction rectifying tower (3); fluidized drying tower(10) The dry desalted high-iron red mud obtained by gas-solid separation at the top of the tower is sent into a fluidized reduction reactor (12) to carry out reduction magnetization reaction with the reduction ironmaking tail gas at 1300-1700 ℃, the reduction tail gas obtained by gas-solid separation of the reduction reaction at the top of the fluidized reduction reactor (12) is used as the fluidized drying gas of a fluidized drying tower (10) after being post-combusted, and the reduced red mud cooler (14) obtained by gas-solid separation at the top of the reduction fluidization reactor (13) is cooled and then subjected to magnetic separation by a magnetic separation separator (15) to recover fine iron ore powder; the refined iron ore powder and the pulverized coal are mixed in a mixing bin (16) and then sent into a Y-shaped entrained flow gasification reduction iron making furnace (17) by using an oxidant, in-situ gasification reduction iron making is carried out at 1300-1700 ℃, high-temperature molten iron, slag and reduction iron making tail gas downwards flow into a settler separator (18) at the bottom of the Y-shaped entrained flow gasification reduction iron making furnace (17), molten iron is obtained from an iron outlet (22) after sedimentation and layering, slag is obtained from a slag outlet (23) and iron making tail gas is sent from an iron making tail gas outlet (21), the iron making tail gas is sent back to a fluidization reduction reactor (12), and the molten iron and slag are discharged outwards as products.|[0025] The Y-type entrained-flow bed gasifying reduction iron-making furnace (17) is operated by fine iron ore powder and pulverized coal according to the proportion of C to Fe 2 O 3 The ratio is 1:1.1 to 4.0 are evenly mixed and sent into a mixing bin (16); the iron coal powder mixture and gasifying agent from the mixing bin (16) are sprayed into a gasification section through a top nozzle (19) and a radial inclined side nozzle (20) of a Y-type entrained-flow bed gasifying reduction iron-making furnace (17), and are gasified and reduced at the temperature of 1300-1700 ℃; the top nozzle (19) and the side nozzle (20) generate a plurality of jet flows which collide with each other in the center of the hearth to form a Y-shaped rotary impact high-temperature reaction zone, the Y-shaped rotary impact high-temperature reaction zone ignites each other to strengthen gasification reduction reaction, ferrocoke residues are thrown to the furnace wall of the gasification section, the rotational flow is downward, the retention and reaction time of the ferrocoke residues in the gasification section is prolonged by more than 20 times, and a solidified slag layer is formed on the surface of a refractory layer of a water-cooled wall of the gasification section to realize slag resistance; the iron-making tail gas, high-temperature molten iron and slag flow to a settler separator (18) through a discharge port in the center of a conical end socket of the gasification section, residual iron ore powder and carbon powder are subjected to thermal insulation for further reduction reaction, and the iron-making tail gas at 1300-1700 ℃ is discharged from an iron-making tail gas outlet (21) on the side surface of the top of the settler separator (18) and pumped into a fluidization reduction reactor (12) for reduction magnetization of high-iron red mud; high heightAfter the hot molten iron and the slag are settled and separated, the slag is discharged through a slag outlet, and the high-temperature molten iron is discharged through a siphon type molten iron outlet (22) and can maintain a stable molten iron-slag interface height.|[0026] The high-iron red mud reaction rectifying dealkalization carbon fixation and reduction ironmaking device provided by the invention realizes the graded utilization of acid gas in flue gas according to the reaction activity by the reaction rectifying tower, efficiently breaks through combustion flue gas decarburization and ultralow emission at low cost, solves the problem of low-cost and high-efficiency removal of insoluble alkaline substances by the high-iron red mud, improves the dealkalization rate from 50% to 98% in general, and ensures that the carbon fixation amount is less than 40KgCO 2 Per ton of 30% red mud is increased to 150KgCO 2 Per ton of red mud above 30%; the dealkalized and carbon-fixed high-iron red mud is subjected to reduction, magnetic separation and in-situ reduction and ironmaking by using the ironmaking tail gas, the purity of iron ore powder is improved by more than 30%, the iron recovery rate is improved by more than 99%, the ironmaking energy consumption is reduced by more than 50%, the cost is reduced by 500-1000 yuan/ton iron, and conditions are created for the high-value utilization of high-iron red mud resources. Family Number|(108513206)|108513206|Abstract|(CN117551832 A)|The invention provides a reactive distillation dealkalization carbon sequestration and reduction ironmaking device for high - iron red mud . The reactive distillation dealkalization carbon sequestration and reduction ironmaking device mainly comprises reactive distillation dealkalization carbon sequestration equipment , fluidized reduction reaction magnetic separation equipment and Y - shaped entrained - flow bed gasifier in - situ reduction ironmaking equipment , the reactive distillation dealkalization and carbon sequestration equipment is of a cross - flow type tower plate structure , the number of tower plates is 1-30 layers of theoretical plates , the distance between the plates is 250-900 mm , a red mud slurry distributor is arranged at the top of the tower , a mixed flue gas distributor is arranged at the bottom of the tower , a purified flue gas outlet is formed in the top of the tower , and a dealkalization and carbon sequestration red mud outlet is formed in the bottom of the tower ; in the fluidized drying - reduction reaction - magnetic separation equipment , a fluidized drying tower is a turbulent fluidized bed , a fluidized reduction reactor is a pulse riser crushing reactor , and a dry magnetic separator is used for magnetic separation ; a cylindrical gasification section is arranged on the upper portion of the Y - shaped entrained - flow bed gasification reduction ironmaking furnace , a cylindrical settler separator is arranged on the lower portion of the Y - shaped entrained - flow bed gasification reduction ironmaking furnace , a top nozzle and a side nozzle are arranged on the top of the gasification section , the nozzles are distributed to be of an inverted - Y - shaped structure , and a slag outlet , a molten iron outlet and an emergency treatment opening are formed in the bottom of the settler separator . |CPC codes|(CN117551832 A)|B01D - 003/14 |B01D - 003/32 |B01D - 053/60 |B01D - 053/62 |B01D - 053/80 |B01D - 2257/504 |B01D - 2258/0283 |IPC codes|(CN117551832 A)|B01D - 003/14 |B01D - 003/32 |B01D - 053/60 |B01D - 053/62 |B01D - 053/80 |Title|(CN117551832 A)|Iron - making device for reactive distillation , dealkalization , carbon sequestration and reduction of high - iron red mud | Chemical engineering|Environmental technology|Materials, metallurgy B01D-003/14|B01D-003/32|B01D-053/60|B01D-053/62|B01D-053/80|B01D-2257/504|B01D-2258/0283|C21B-013/00/26|C21B-013/00/33|C21B-013/00/73|C21B-013/14|C21B-2100/62|C22B-001/00/5|C22B-007/00/6|C22B-021/00/07|C22B-021/00/23 B01D-003/14|B01D-003/32|B01D-053/60|B01D-053/62|B01D-053/80|B01D-2257/504|B01D-2258/0283|C21B-013/00/26|C21B-013/00/33|C21B-013/00/73|C21B-013/14|C21B-2100/62|C22B-001/00/5|C22B-007/00/6|C22B-021/00/07|C22B-021/00/23 B01D-003/14|B01D-003/32|B01D-053/60|B01D-053/62|B01D-053/80|C21B-013/00|C21B-013/14|C22B-001/00|C22B-007/00|C22B-021/00 B01D-003/14|B01D-003/32|B01D-053/60|B01D-053/62|B01D-053/80|C21B-013/00|C21B-013/14|C22B-001/00|C22B-007/00|C22B-021/00 PENDING (CN117551832)|PENDING ALIVE (CN117551832)|ALIVE (CN117551832)|LEGAL DETAILS FOR CN117551832|Actual or expected expiration date=2043-12-19|Legal state=ALIVE|Status=PENDING|Event publication date=2023-12-19|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202311752222|Application date=2023-12-19|Standardized application number=2023CN-1752222|Event publication date=2024-02-13|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN117551832|Publication stage code=A|Publication date=2024-02-13|Standardized publication number=CN117551832|Event publication date=2024-02-13|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-03-01|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN117551832)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQbbMDrsgfOp1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000071444822&ekey=2013&xpn=CN117551832&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=hY7EILabNk46I6OMPIfQh5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN117551832)|CN (CN117551832)|NAME=CHINA UNIVERSITY OF PETROLEUM (EAST CHINA) , COUNTRY=CN (CN117551832)|NAME=TIAN YUANYU|NAME=QIAO YINGYUN|NAME=TIAN YILIANG|NAME=ZHANG YANPENG|NAME=YE ZHIGANG 0 1 Titre: (CN117551832)|Iron-making device for reactive distillation, dealkalization, carbon sequestration and reduction of high-iron red mud Résumé: (CN117551832)|The invention provides a reactive distillation dealkalization carbon sequestration and reduction ironmaking device for high-iron red mud. The reactive distillation dealkalization carbon sequestration and reduction ironmaking device mainly comprises reactive distillation dealkalization carbon sequestration equipment, fluidized reduction reaction magnetic separation equipment and Y-shaped entrained-flow bed gasifier in-situ reduction ironmaking equipment, the reactive distillation dealkalization and carbon sequestration equipment is of a cross-flow type tower plate structure, the number of tower plates is 1-30 layers of theoretical plates, the distance between the plates is 250-900 mm, a red mud slurry distributor is arranged at the top of the tower, a mixed flue gas distributor is arranged at the bottom of the tower, a purified flue gas outlet is formed in the top of the tower, and a dealkalization and carbon sequestration red mud outlet is formed in the bottom of the tower; in the fluidized drying-reduction reaction-magnetic separation equipment, a fluidized drying tower is a turbulent fluidized bed, a fluidized reduction reactor is a pulse riser crushing reactor, and a dry magnetic separator is used for magnetic separation; a cylindrical gasification section is arranged on the upper portion of the Y-shaped entrained-flow bed gasification reduction ironmaking furnace, a cylindrical settler separator is arranged on the lower portion of the Y-shaped entrained-flow bed gasification reduction ironmaking furnace, a top nozzle and a side nozzle are arranged on the top of the gasification section, the nozzles are distributed to be of an inverted-Y-shaped structure, and a slag outlet, a molten iron outlet and an emergency treatment opening are formed in the bottom of the settler separator. 1 Abstract gpt-4o-mini no The patent focuses on an iron-making device and processes related to iron production and red mud treatment, rather than on accelerating mineral weathering for CO₂ capture.
3 CN202510651543 CN202510651543 CN120345407|CN120345407 115358899 CN120345407 B 2025-11-28 [CN120345407B]|CN120345407 A 2025-07-22 [CN120345407] 2025-05-20 2025-05-20 2025-11-28|2025-07-22 (CN120345407B)|2025-11-28 (CN120345407)|2045-05-20 (CN120345407)|Rice field straw returning method for carbon fixation and emission reduction (CN120345407)|The invention relates to the technical field of agricultural environmental protection, in particular to a carbon sequestration and emission reduction rice field straw returning method, which comprises the following steps: performing multistage crushing pretreatment on straws, mixing with red mud, performing gradient pyrolysis to prepare magnetic biochar, fixing specific strains, returning to the field, constructing a three-layer stubble burying structure to improve soil, and performing sensor monitoring and neural network regulation. And carbon sequestration emission reduction and intelligent management are realized, and the carbon flow direction can be tracked and a carbon sink voucher can be generated. According to the invention, through straw pretreatment, biochar preparation and fungus-carbon coupling returning, efficient carbon sequestration and emission reduction can be realized; the three-layer stubble burying structure is matched with humic acid, so that the soil structure is improved, the air permeability and water and fertilizer retention performance are improved, and crop growth is facilitated; by means of sensor monitoring and neural network regulation and control, precise management is achieved, carbon metering is conducted by combining isotope labeling with the block chain, data are accurate and safe, and powerful support is provided for carbon transactions and the like. XINGAN LEAGUE AGRICULTURE & ANIMAL HUSBANDRY ACAD (CN120345407)|AGRICULTURAL AND PASTORAL SCIENCE RES INSTITUTE OF XHINGAN UNION ([CN])|(CN120345407)|AGRICULTURAL AND PASTORAL SCIENCE RES INSTITUTE OF XHINGAN UNION ([CN]) XU XINGJIAN|BAI LU|GU YANRU|WEN LI|SUN WURINA|LIANG SHUANG|XUE HAINAN|HAN LEI|LIU JICONG|LIANG YI|NING XIAOMENG|MA BENCHI|LUO WEI|HAN FENG (CN120345407)|Xu Xingjian|Bai Lu|Gu Yanru|Wen Li|Sun Wurina|Liang Shuang|Xue Hainan|Han Lei|Liu Jicong|Liang Yi|Ning Xiaomeng|Ma Benchi|Luo Wei|Han Feng|(CN120345407)|XU XINGJIAN|BAI LU|GU YANRU|WEN LI|SUN WURINA|LIANG SHUANG|XUE HAINAN|HAN LEI|LIU JICONG|LIANG YI|NING XIAOMENG|MA BENCHI|LUO WEI|HAN FENG (CN120345407)|TIAN YUXUAN;SHENZHEN FENG CHENG ZHI HE INTELLECTUAL PROPERTY AGENCY CO. LTD|Reg. Nb: 44525 (CN120345407)|Compared with the prior art, the technical proposal provided by the invention has the following advantages that|Key indexes such as Eh value, CH _4 concentration and microbial activity of soil cannot be mastered in time, irrigation and fertilization strategies are difficult to adjust according to actual conditions of the soil, and resource waste and environmental pollution are caused.|The common returning mode lacks scientific regulation and control on straw treatment and microorganism utilization, so that the methane emission is large, the carbon fixation efficiency is extremely low, and the ever-increasing carbon emission reduction requirement worldwide is difficult to meet.In terms of soil improvement, it is difficult to effectively improve the soil structure by conventional methods.|The non-embedding of comparative example 2 causes the death of the microbial inoculum, and the emission reduction efficiency is greatly reduced.| (CN120345407)|1. A carbon fixation and emission reduction rice field straw returning method is characterized by comprising the following steps: S1, straw multistage crushing and pretreatment, namely finishing rice harvesting by adopting a double-knife roller differential harvesting and crushing integrated machine, longitudinally cutting by a front knife roller to form a straw section of 5-8cm, and transversely kneading by a rear knife roller to ensure that the fiber cracking degree is more than or equal to 85 percent and the crushing uniformity variation coefficient is less than or equal to 10 percent; S2, gradient activation preparation of biological carbon, namely mixing the straw obtained in the step S1 with a red mud catalyst according to the doping amount of 5-8%, and carrying out three-stage gradient pyrolysis under a mixed atmosphere with the volume ratio of CO 2 to N 2 of 1:3, wherein the three-stage gradient pyrolysis is specifically 200 ℃ per 30min to 400 ℃ per 1h to 550 ℃ per 2h, so as to generate the magnetic biological carbon with the specific surface area of more than or equal to 120m 2/g and the pore size distribution of a micropore and mesopore composite structure, wherein micropores are less than 2nm, mesopores are 2-50nm, and the Fe 3O4 load amount in the magnetic biological carbon is 3-5%; S3, bacteria-carbon coupling returning, namely fixing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria in the pores of the biochar according to the proportion of 1:2, and applying a biochar-bacteria complex according to the proportion of 20-30% of the dry weight of the straw, wherein the survival rate of bacteria is more than or equal to 90%/30 days; S4, three-dimensional stubble burying and soil improvement, namely, constructing a three-layer stubble burying structure by adopting a hydraulic turnover plow and a rotary cultivator to perform combined operation, wherein the three-layer stubble burying structure comprises a biological carbon mixed layer with the surface layer of 0-10cm, a straw-bacterial agent composite layer with the middle layer of 10-25cm and a red mud solidified layer with the bottom layer of 25-40cm, and a humic acid binder is applied in a matched manner to form a honeycomb pore structure; S5, intelligent regulation and carbon metering, namely, deploying a sensor array for LoRa communication, monitoring the Eh value, CH 4 concentration and microbial activity of the soil in real time, dynamically adjusting an irrigation strategy and the activation frequency of a microbial inoculum through a convolutional neural network, and synchronously tracking the carbon flow direction of the straw by using delta 13 C isotope labeling and generating a blockchain carbon sink certificate. | (CN120345407)|Aiming at the defects existing in the prior art, the invention provides a carbon-fixing and emission-reducing rice field straw returning method, which can efficiently fix carbon and reduce emission through straw pretreatment, biochar preparation and fungus-carbon coupling returning; the three-layer stubble burying structure is matched with humic acid, improves the soil structure, improves the ventilation, water and fertilizer retention performance of the soil structure, is beneficial to crop growth, realizes accurate management by means of sensor monitoring and neural network regulation and control, performs carbon metering by combining isotope labeling with blockchain, has accurate and safe data, and provides powerful support for carbon transaction and the like.|The invention relates to the technical field of agricultural environmental protection, in particular to a carbon fixation and emission reduction rice field straw returning method.|The invention relates to the technical field of agricultural environmental protection, in particular to a method for returning rice field straws with carbon fixation and emission reduction, which comprises the steps of carrying out multistage crushing pretreatment on the straws, mixing with red mud, carrying out gradient pyrolysis to prepare magnetic biochar, fixing specific strains, returning to the field, constructing three-layer stubble burying structure improved soil, realizing carbon fixation, emission reduction and intelligent management through sensor monitoring and neural network regulation, and tracking carbon flow direction and generating carbon sink certificates.| (CN120345407)|EMISSION REDUCTION(100,22)|CARBON FIXATION(100,12)|RICE FIELD STRAW(100,5)|MULTISTAGE CRUSHING PRETREATMENT(100,2)|MICROBIAL INOCULUM DEATH(99,1)|STRAW MULTISTAGE CRUSHING(84,3)|MICROBIAL INOCULUM(80,10)|NEURAL NETWORK REGULATION(73,3)|INTELLIGENT MANAGEMENT(71,1)|HYDRAULIC TURNOVER PLOW(67,4)|FERTILIZATION STRATEGY(67,1)|AGRICULTURAL ENVIRONMENTAL PROTECTION(66,2)|FERTILIZER RETENTION PERFORMANCE(66,2)|GRADIENT PYROLYSIS(62,8)|STRAW PRETREATMENT(62,1)|MONITORING SENSOR(61,3)|STRAW(60,22)|BIOCHAR PORE(58,3)|MICROBIAL INOCULUM ACTIVATION FREQUENCY(58,3)|INTELLIGENT REGULATION(57,9)|STUBBLE BURYING(57,3)|KNIFE ROLLER(56,6)|COMPOSITE MICROBIAL INOCULUM(56,1)|MICROORGANISM UTILIZATION(55,1)|IRRIGATION STRATEGY(54,3)|SCIENTIFIC REGULATION(54,1)|CARBON GRADIENT ACTIVATION(50,2)|HALOPHILIC METHANE OXIDIZING BACTERIUM(47,4)|ACCURATE MANAGEMENT(46,3)|RESOURCE WASTE(46,1)|STRAW CARBON FINGERPRINT DATABASE(45,2)|BIOCHAR BACTERIUM COMPLEX(44,2)|HYPERLEDGERFABRIC PRIVATE(44,2)|CARBON SEQUESTRATION(42,7)|BIOCHAR POROSITY(42,2)|RED MUD CATALYST(41,9)|MAGNETIC CARBON(41,4)|VENTILATION(40,7)|ISOTOPE LABELING(40,6)|GRADIENT ACTIVATION(40,4)|CARBON TRANSACTION(39,4)|STRAW TREATMENT(39,1)|CARBON SINK CERTIFICATE(38,2)|RESISTANT CELLULOSE(38,2)|TAMPER PROOF CREDENTIAL(38,2)|CARBON METERING(37,7)|HYPERLEDGERFABRIC ARCHITECTURE(37,3)|LORA COMMUNICATION(37,3)|ROLLER DIFFERENTIAL(36,2)|UHFRFID LABEL(36,2)|TECHNICAL PROPOSAL(35,2)|STRAIN(35,1)|POWERFUL SUPPORT(34,2)|GROUND(33,10)|EH VALUE(33,3)|DOUBLE KNIFE ROLLER DIFFERENTIAL(33,2)|ENVIRONMENTAL PROTECTION(33,2)|MICROPORE PORE SIZE DISTRIBUTION(33,2)|RED MUD CATALYST DOPING(33,2)|ACTIVATION FREQUENCY(32,2)|PIEZOELECTRIC CERAMIC(32,2)|STRAW COLLECTION(32,2)|SODIUM ALGINATE BIOCHAR COMPOSITE(31,4)|MICRO AEROBIC ENVIRONMENT(30,4)|MULTISPECTRAL UNMANNED AERIAL VEHICLE(30,3)|CARBON SINK CERTIFICATE GENERATION(30,1)|GEL MICROSPHERE(29,3)|GPS COORDINATE(29,3)|STRAW DRY WEIGHT(29,3)|HUMIC ACID BINDER(28,4)|CERTIFICATE(28,2)|MESOPORE(28,2)|NDVI INDEX(28,2)|LSTM NEURAL NETWORK MODEL(27,4)|FE MOLAR RATIO(27,1)|RETURN MODE(27,1)|METHANE OXIDIZING BACTERIUM(26,6)|MICROPORE(26,3)|BIOCHAR PRODUCTION(26,2)|CROP GROWTH(26,2)|GRADIENT OXYGEN ENVIRONMENT(26,2)|MESOPORE COMPOSITE STRUCTURE(26,2)|MICROBIAL CELL(26,2)|RED MUD DOPING(25,3)|ENVIRONMENTAL POLLUTION(25,1)|METHANE EMISSION(25,1)|MIXED ATMOSPHERE(24,3)|PRETREATMENT(24,3)|THREE DIMENSIONAL STUBBLE BURYING(24,3)|GEL PRECURSOR(24,2)|ACCURATE DATA(24,1)|CARBON EMISSION REDUCTION REQUIREMENT(24,1)|THREE LAYER STUBBLE(23,9)|RED MUD(23,7)|BIOCHAR(23,5)|PORE SIZE(23,5)|THREE STAGE GRADIENT PYROLYSIS(23,5)|HONEYCOMB PORE STRUCTURE(23,4)|BACTERIUM CARBON COUPLING(23,3)|DOPING(23,3)|CARBON SINK(22,10)|ELECTRIC CONTROL MICROBIAL INOCULUM(22,4)|SOIL IMPROVEMENT(22,4)|AGENT COMPOSITE LAYER(22,3)|BACTERIA(22,3)|INTEGRATED MACHINE(22,3)|IRRIGATION(22,2)|RETURNING RICE FIELD STRAW(22,1)|HUMIC ACID(21,5)|ROTARY CULTIVATOR(21,4)|COPRECIPITATION(21,3)|MODEL PARAMETER OPTIMIZATION(21,2)|BLOCK CHAIN(20,4)|FIBER CRACKING DEGREE(20,3)|MIDDLE LAYER(20,3)|DEFECT(20,2)|FUNGUS CARBON COUPLING(20,2)|SAFE DATA(20,1)|STRAW SECTION(19,3)|MICROFLUIDIC(19,2)|RICE(19,2)|CONVOLUTIONAL NEURAL NETWORK(18,4)|SOIL STRUCTURE(18,4)|FOG DIAMETER(18,2)|PRIVACY DATA(18,2)|AREA ADAPTATION MODEL(18,1)|DRY WEIGHT(17,3)|BLOCK CHAIN CARBON SINK(17,2)|MIXING MAGNETIC(17,2)|MICROWAVE ENERGY MONITORING(16,3)|MACHINE LEARNING MODEL(16,2)|EMISSION REDUCTION RICE FIELD(15,10)|MATCH DEGREE(15,4)|THALLUS SIZE(15,2)|CARBON FIXING(15,1)|FULL LIFE CYCLE MANAGEMENT(14,1)|MICROBIAL INOCULUM IMMOBILIZATION(14,1)|MICROWAVE POWER DENSITY(13,7)|BIOCHAR PREPARATION(13,2)|CARBONIZATION(13,2)|CORE DISSOLVED OXYGEN(13,2)|DAMP HEAT CLIMATE ZONE(13,2)|DATA COLLECTION(13,2)|LNAOH(13,2)|SLOW RELEASE NUTRITION SOURCE(13,2)|SODIUM ALGINATE SOLUTION(13,2)|GATEWAY(12,3)|INFRARED IMAGE(12,3)|LASER ABLATION(12,3)|MODEL OUTPUT(12,2)|CARRYING OUT GRADIENT PYROLYSIS(12,1)|HALOPHILIC BACTERIA PROPORTION(12,1)|RICE FIELD(11,11)|SURVIVAL RATE(11,4)|ISOTOPE MASS SPECTROMETRY(11,3)|CARBON MIXED LAYER(11,2)|MIXED GAS(11,2)|SALINE ALKALI SOIL ADAPTATION(11,2)|BIOCHAR GRADIENT ACTIVATION(11,1)|MICROBIAL INOCULUM PARAMETER(11,1)|SOIL FERTILIZER RETENTION(11,1)|STRAW INSUFFICIENT DECOMPOSITION(11,1)|SENSOR ARRAY(10,4)|PORE DIAMETER MATCHING DEGREE(10,2)|SALINE ALKALI AREA(10,2)|BOTTOM LAYER(9,5)|DELTA 13C ISOTOPE LABELING(9,3)|AGRICULTURAL CARBON TRANSACTION MARKET(9,1)|AGRICULTURAL ECOLOGICAL ENVIRONMENT(9,1)|TRACEABLE METERING(9,1)|POROSITY(8,6)|STRAW CARBON FLOW DIRECTION(8,3)|CARBON SINK CREDENTIAL GENERATION(8,2)|CARBON SINK DATA(8,2)|AGRICULTURE GREEN SUSTAINABLE DEVELOPMENT(8,1)|CARBON ASSET TRANSACTION SAFETY(8,1)|CARBON TRANSACTION AUTHENTICATION REQUIREMENT(8,1)|COMPOUND MICROBIAL INOCULUM(8,1)|CRUSHING PRETREATMENT(8,1)|IRRIGATION MANAGEMENT(8,1)|SEED UNIFORMITY(8,1)|VENTILATION HIDDEN PIPE(8,1)|HYDROCHLORIC ACID(7,3)|THREE DIMENSIONAL EMISSION MODEL(7,3)|VOLUME RATIO(7,3)|TRACKING CARBON FLOW DIRECTION(7,2)|ARTIFICIAL IRRIGATION(7,1)|ATP DETECTOR ACCURACY(7,1)|COLLECT NDVI(7,1)|FARMLAND MANAGEMENT(7,1)|HARVESTING RICE(7,1)|HUMID CLIMATE ZONE(7,1)|IRRIGATION PRECISION(7,1)|MODIFYING BIOCHAR(7,1)|PEAK PREDICTION PRECISION(7,1)|RESOURCE UTILIZATION(7,1)|STRAW DECOMPOSITION(7,1)|TEMPERATURE RESISTANT CELLULOLYTIC BACTERIUM(7,1)|YARN KNEADING TREATMENT(7,1)|SURFACE LAYER(6,4)|ZERO KNOWLEDGE PROOF(6,4)|INPUT PARAMETER(6,2)|MASS RATIO(6,2)|ACCURATE METERING(6,1)|BIOCHAR FUNGICIDE COMPLEX(6,1)|CONCEALED PIPE(6,1)|DEPLOYING SENSOR(6,1)|DYNAMIC REGULATION(6,1)|FUNGUS AGENT(6,1)|GUARANTEEING SAFETY(6,1)|HOT CLIMATE ZONE ADAPTATION(6,1)|INOCULUM ACTIVATION FREQUENCY(6,1)|LSTM MODEL(6,1)|MICROBIAL INOCULUM SURVIVAL RATE(6,1)|NAOH MODIFICATION(6,1)|SCIENTIFIC CARBON(6,1)|SOIL KEY INDEX(6,1)|STRAW DENSITY(6,1)|STRAW TURNING(6,1)|UNIFORMITY COEFFICIENT(6,1)|STANDING WAVE RATIO(5,3)|DISSOLVED OXYGEN GRADIENT(5,2)|DISSOLVED OXYGEN SURFACE(5,2)|MODIFIED RED MUD CATALYST(5,2)|SOLID LIQUID RATIO(5,2)|ACCURATE AGRICULTURAL MANAGEMENT(4,1)||(CN120345407)|EMISSION REDUCTION(100,15)|STRAW(100,15)|CARBON FIXATION(100,11)|RICE FIELD(100,5)|RICE FIELD STRAW(100,5)|EMISSION REDUCTION RICE FIELD(100,4)|MULTISTAGE CRUSHING PRETREATMENT(100,2)|MICROBIAL INOCULUM DEATH(99,1)|HALOPHILIC METHANE OXIDIZING BACTERIUM(96,4)|STRAW MULTISTAGE CRUSHING(84,3)|METHANE OXIDIZING BACTERIUM(81,6)|MICROBIAL INOCULUM(80,10)|CELLULOSE DECOMPOSING BACTERIUM(80,2)|RESISTANT CELLULOSE DECOMPOSING BACTERIUM(80,2)|NEURAL NETWORK REGULATION(73,3)|INTELLIGENT MANAGEMENT(71,1)|HYDRAULIC TURNOVER PLOW(67,4)|FERTILIZATION STRATEGY(67,1)|AGRICULTURAL ENVIRONMENTAL PROTECTION(66,2)|FERTILIZER RETENTION PERFORMANCE(66,2)|GRADIENT PYROLYSIS(62,8)|DECOMPOSING BACTERIA(62,2)|STRAW PRETREATMENT(62,1)|MONITORING SENSOR(61,3)|BIOCHAR PORE(58,3)|MICROBIAL INOCULUM ACTIVATION FREQUENCY(58,3)|INTELLIGENT REGULATION(57,9)|STUBBLE BURYING(57,3)|KNIFE ROLLER(56,6)|MICROORGANISM UTILIZATION(55,1)|IRRIGATION STRATEGY(54,3)|SCIENTIFIC REGULATION(54,1)|CARBON GRADIENT ACTIVATION(50,2)|METHANE EMISSION(47,1)|ACCURATE MANAGEMENT(46,3)|RESOURCE WASTE(46,1)|STRAW CARBON FINGERPRINT DATABASE(45,2)|SODIUM ALGINATE BIOCHAR COMPOSITE(44,3)|BIOCHAR BACTERIUM COMPLEX(44,2)|HYPERLEDGERFABRIC PRIVATE(44,2)|BIOCHAR POROSITY(42,2)|RED MUD CATALYST(41,9)|MAGNETIC CARBON(41,4)|VENTILATION(40,7)|ISOTOPE LABELING(40,6)|GRADIENT ACTIVATION(40,4)|CARBON TRANSACTION(39,4)|COMPOUND MICROBIAL INOCULUM(39,2)|STRAW TREATMENT(39,1)|CARBON SINK CERTIFICATE(38,2)|SODIUM ALGINATE BIOCHAR COMPOUND(38,2)|TAMPER PROOF CREDENTIAL(38,2)|CARBON METERING(37,7)|HYPERLEDGERFABRIC ARCHITECTURE(37,3)|LORA COMMUNICATION(37,3)|ROLLER DIFFERENTIAL(36,2)|UHFRFID LABEL(36,2)|TECHNICAL PROPOSAL(35,2)|STRAIN(35,1)|POWERFUL SUPPORT(34,2)|GROUND(33,10)|EH VALUE(33,3)|DOUBLE KNIFE ROLLER DIFFERENTIAL(33,2)|ENVIRONMENTAL PROTECTION(33,2)|MICROPORE PORE SIZE DISTRIBUTION(33,2)|RED MUD CATALYST DOPING(33,2)|BIOCHAR(32,6)|ACTIVATION FREQUENCY(32,2)|PIEZOELECTRIC CERAMIC(32,2)|STRAW COLLECTION(32,2)|MICRO AEROBIC ENVIRONMENT(30,4)|MULTISPECTRAL UNMANNED AERIAL VEHICLE(30,3)|GEL MICROSPHERE(29,3)|GPS COORDINATE(29,3)|STRAW DRY WEIGHT(29,3)|CERTIFICATE(28,2)|MESOPORE(28,2)|NDVI INDEX(28,2)|LSTM NEURAL NETWORK MODEL(27,4)|FE MOLAR RATIO(27,1)|RETURN MODE(27,1)|HUMIC ACID BINDER(26,4)|MICROPORE(26,3)|BIOCHAR PRODUCTION(26,2)|CROP GROWTH(26,2)|GRADIENT OXYGEN ENVIRONMENT(26,2)|MESOPORE COMPOSITE STRUCTURE(26,2)|MICROBIAL CELL(26,2)|HUMIC ACID(25,9)|CARBON SINK CREDENTIAL GENERATION(25,3)|RED MUD DOPING(25,3)|ENVIRONMENTAL POLLUTION(25,1)|MIXED ATMOSPHERE(24,3)|PRETREATMENT(24,3)|THREE DIMENSIONAL STUBBLE BURYING(24,3)|GEL PRECURSOR(24,2)|ACCURATE DATA(24,1)|CARBON EMISSION REDUCTION REQUIREMENT(24,1)|THREE LAYER STUBBLE(23,9)|RED MUD(23,7)|PORE SIZE(23,5)|THREE STAGE GRADIENT PYROLYSIS(23,5)|HONEYCOMB PORE STRUCTURE(23,4)|BACTERIUM CARBON COUPLING(23,3)|DOPING(23,3)|CARBON SINK(22,10)|ELECTRIC CONTROL MICROBIAL INOCULUM(22,4)|SOIL IMPROVEMENT(22,4)|AGENT COMPOSITE LAYER(22,3)|INTEGRATED MACHINE(22,3)|IRRIGATION(22,2)|REGION ADAPTATION MODEL(22,2)|RETURNING RICE FIELD STRAW(22,1)|ROTARY CULTIVATOR(21,4)|COPRECIPITATION(21,3)|MODEL PARAMETER OPTIMIZATION(21,2)|BLOCK CHAIN(20,4)|FIBER CRACKING DEGREE(20,3)|MIDDLE LAYER(20,3)|DEFECT(20,2)|FUNGUS CARBON COUPLING(20,2)|SAFE DATA(20,1)|CONVOLUTIONAL NEURAL NETWORK(19,4)|STRAW SECTION(19,3)|MICROFLUIDIC(19,2)|RICE(19,2)|SOIL STRUCTURE(18,4)|FOG DIAMETER(18,2)|PRIVACY DATA(18,2)|DRY WEIGHT(17,3)|BLOCK CHAIN CARBON SINK(17,2)|MICROWAVE ENERGY MONITORING(16,3)|MACHINE LEARNING MODEL(16,2)|MATCH DEGREE(15,4)|THALLUS SIZE(15,2)|CARBON FIXING(15,1)|CARBON SEQUESTRATION(15,1)|MICROBIAL INOCULUM IMMOBILIZATION(14,1)|MICROWAVE POWER DENSITY(13,7)|CARBONIZATION(13,2)|CORE DISSOLVED OXYGEN(13,2)|DAMP HEAT CLIMATE ZONE(13,2)|DATA COLLECTION(13,2)|LNAOH(13,2)|SLOW RELEASE NUTRITION SOURCE(13,2)|SODIUM ALGINATE SOLUTION(13,2)|GATEWAY(12,3)|INFRARED IMAGE(12,3)|LASER ABLATION(12,3)|HEATING RATE MINUTE(12,2)|MODEL OUTPUT(12,2)|CARRYING OUT GRADIENT PYROLYSIS(12,1)|HALOPHILIC BACTERIA PROPORTION(12,1)|SURVIVAL RATE(11,4)|ISOTOPE MASS SPECTROMETRY(11,3)|CARBON MIXED LAYER(11,2)|MIXED GAS(11,2)|SALINE ALKALI SOIL ADAPTATION(11,2)|BIOCHAR GRADIENT ACTIVATION(11,1)|MICROBIAL INOCULUM PARAMETER(11,1)|SOIL FERTILIZER RETENTION(11,1)|STRAW INSUFFICIENT DECOMPOSITION(11,1)|SENSOR ARRAY(10,4)|PORE DIAMETER MATCHING DEGREE(10,2)|SALINE ALKALI AREA(10,2)|BOTTOM LAYER(9,5)|DELTA 13C ISOTOPE LABELING(9,3)|AGRICULTURAL CARBON TRANSACTION MARKET(9,1)|AGRICULTURAL ECOLOGICAL ENVIRONMENT(9,1)|TRACEABLE METERING(9,1)|POROSITY(8,6)|STRAW CARBON FLOW DIRECTION(8,3)|CARBON SINK DATA(8,2)|AGRICULTURE GREEN SUSTAINABLE DEVELOPMENT(8,1)|CARBON ASSET TRANSACTION SAFETY(8,1)|CARBON TRANSACTION AUTHENTICATION REQUIREMENT(8,1)|CRUSHING PRETREATMENT(8,1)|IRRIGATION MANAGEMENT(8,1)|SEED UNIFORMITY(8,1)|VENTILATION HIDDEN PIPE(8,1)|HYDROCHLORIC ACID(7,3)|THREE DIMENSIONAL EMISSION MODEL(7,3)|VOLUME RATIO(7,3)|TRACKING CARBON FLOW DIRECTION(7,2)|ARTIFICIAL IRRIGATION(7,1)|ATP DETECTOR ACCURACY(7,1)|COLLECT NDVI(7,1)|FARMLAND MANAGEMENT(7,1)|HARVESTING RICE(7,1)|HUMID CLIMATE ZONE(7,1)|IRRIGATION PRECISION(7,1)|MODIFYING BIOCHAR(7,1)|OXIDIZING BACTERIA(7,1)|PEAK PREDICTION PRECISION(7,1)|RESOURCE UTILIZATION(7,1)|STRAW DECOMPOSITION(7,1)|TEMPERATURE RESISTANT CELLULOLYTIC BACTERIUM(7,1)|YARN KNEADING TREATMENT(7,1)|SURFACE LAYER(6,4)|ZERO KNOWLEDGE PROOF(6,4)|INPUT PARAMETER(6,2)|MASS RATIO(6,2)|ACCURATE METERING(6,1)|BIOCHAR FUNGICIDE COMPLEX(6,1)|CONCEALED PIPE(6,1)|DEPLOYING SENSOR(6,1)|DYNAMIC REGULATION(6,1)|FUNGUS AGENT(6,1)|GUARANTEEING SAFETY(6,1)|HOT CLIMATE ZONE ADAPTATION(6,1)|INOCULUM ACTIVATION FREQUENCY(6,1)|LSTM MODEL(6,1)|MICROBIAL INOCULUM SURVIVAL RATE(6,1)|SCIENTIFIC CARBON(6,1)|SOIL KEY INDEX(6,1)|STRAW DENSITY(6,1)|STRAW TURNING(6,1)|UNIFORMITY COEFFICIENT(6,1)|STANDING WAVE RATIO(5,3)|DISSOLVED OXYGEN GRADIENT(5,2)|DISSOLVED OXYGEN SURFACE(5,2)|MODIFIED RED MUD CATALYST(5,2)|SOLID LIQUID RATIO(5,2)|ACCURATE AGRICULTURAL MANAGEMENT(4,1)|ACCURATE CARBON METERING(4,1)| (CN120345407)|1. A carbon fixation and emission reduction rice field straw returning method is characterized by comprising the following steps:| S1, straw multistage crushing and pretreatment, namely finishing rice harvesting by adopting a double-knife roller differential harvesting and crushing integrated machine, longitudinally cutting by a front knife roller to form a straw section of 5-8cm, and transversely kneading by a rear knife roller to ensure that the fiber cracking degree is more than or equal to 85 percent and the crushing uniformity variation coefficient is less than or equal to 10 percent; | S2, gradient activation preparation of biological carbon, namely mixing the straw obtained in the step S1 with a red mud catalyst according to the doping amount of 5-8%, and carrying out three-stage gradient pyrolysis under a mixed atmosphere with the volume ratio of CO 2 to N 2 of 1:3, wherein the three-stage gradient pyrolysis is specifically 200 ℃ per 30min to 400 ℃ per 1h to 550 ℃ per 2h, so as to generate the magnetic biological carbon with the specific surface area of more than or equal to 120m 2/g and the pore size distribution of a micropore and mesopore composite structure, wherein micropores are less than 2nm, mesopores are 2-50nm, and the Fe 3O4 load amount in the magnetic biological carbon is 3-5%; | S3, bacteria-carbon coupling returning, namely fixing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria in the pores of the biochar according to the proportion of 1:2, and applying a biochar-bacteria complex according to the proportion of 20-30% of the dry weight of the straw, wherein the survival rate of bacteria is more than or equal to 90%/30 days; | S4, three-dimensional stubble burying and soil improvement, namely, constructing a three-layer stubble burying structure by adopting a hydraulic turnover plow and a rotary cultivator to perform combined operation, wherein the three-layer stubble burying structure comprises a biological carbon mixed layer with the surface layer of 0-10cm, a straw-bacterial agent composite layer with the middle layer of 10-25cm and a red mud solidified layer with the bottom layer of 25-40cm, and a humic acid binder is applied in a matched manner to form a honeycomb pore structure; | S5, intelligent regulation and carbon metering, namely, deploying a sensor array for LoRa communication, monitoring the Eh value, CH 4 concentration and microbial activity of the soil in real time, dynamically adjusting an irrigation strategy and the activation frequency of a microbial inoculum through a convolutional neural network, and synchronously tracking the carbon flow direction of the straw by using delta 13 C isotope labeling and generating a blockchain carbon sink certificate. |2. The carbon sequestration and emission reduction rice field straw returning method according to claim 1, wherein the red mud catalyst in the step S2 is modified by hydrochloric acid with a concentration of 0.5mol/L, wherein the solid-liquid ratio is 1:5, the specific surface area is increased to 150m 2/g, the magnetic load realizes a molar ratio of Fe 2+/Fe3 + of 1:2 by a coprecipitation method, and the strength of an external magnetic field is 0.5T.|3. The carbon fixation and emission reduction rice field straw returning method according to claim 1, wherein the microbial inoculum is immobilized by adopting a sodium alginate-biochar composite gel embedding technology, the matching degree of pore size distribution and the size of the microbial cells is more than or equal to 90%, and a micro-aerobic environment is constructed to maintain the activity of methane oxidizing bacteria, and the dissolved oxygen of the micro-aerobic environment is 0.5-1.5mg/L.|4. The carbon sequestration and emission reduction rice field straw returning method according to claim 1, wherein the intelligent regulation system comprises:| the multispectral unmanned aerial vehicle collects the NDVI index and the thermal infrared image of the paddy field every week, and a three-dimensional emission model is built; | The edge computing gateway runs an LSTM neural network model, wherein the prediction precision R 2 is more than or equal to 0.92; | The response time of the water valve driven by the piezoelectric ceramic and the electric control microbial inoculum atomizing nozzle is less than or equal to 50ms, and the diameter of fog drops of the electric control microbial inoculum atomizing nozzle is 50-80 mu m. |5. The carbon sequestration and emission reduction rice field straw returning method according to claim 1, wherein the area adaptation model is established:| in a damp-heat climate zone, the red mud doping amount is increased to 10 percent, and ventilation concealed pipes are arranged, wherein the distance between the ventilation concealed pipes is 1.5m; | in the saline-alkali area, the porosity of the biochar is improved by 40% through modification of 1 mol/LNaOH. |6. The carbon sequestration and emission reduction rice field straw returning method according to claim 1, wherein the full life cycle management comprises:| The UHFRFID label is adopted in the straw collection stage to track the water content and the heat value; | A microwave energy monitoring system is deployed in the biochar production stage, wherein the standing wave ratio is less than or equal to 1.5; | the carbon sink data generates a tamper-proof credential through HyperledgerFabric architecture. |7. The carbon sequestration and emission reduction rice field straw returning method according to claim 1, wherein the composite microbial inoculum in the step S3 adopts a sodium alginate-biochar composite gel embedding technology, and specifically comprises the following steps:| Mixing magnetic biochar with sodium alginate solution according to a mass ratio of 1:3 to form a gel precursor; | Gel microspheres with the particle size of 50-200 mu m are prepared by a microfluidic technology, and the matching degree of the pore diameter and the thallus size is more than or equal to 90%; | the gradient oxygen environment is built in the gel microsphere, specifically, 1.5-2.0mg/L of surface dissolved oxygen, 0.3-0.8mg/L of core dissolved oxygen and 0.5-1.0% humic acid are synchronously loaded as a slow-release nutrition source. |8. The carbon sequestration and emission reduction rice field straw returning method according to claim 2, wherein the biochar preparation process in step S2 is dynamically regulated and controlled by a machine learning model, and specifically comprises:| Constructing an LSTM neural network model, wherein input parameters comprise 8-12% of straw water content, 5-8% of red mud catalyst doping amount and 10-20 ℃ per minute of heating rate; | Collecting data of the flow rate of mixed gas of CO 2 and N 2 of 0.8-1.2m/s and the specific surface area of a product in real time in the carbonization process, optimizing model parameters through transfer learning, and predicting the accuracy R 2 to be more than or equal to 0.93; | And dynamically adjusting the microwave power density and the injection rate of the activating agent NH 3 according to the model output, wherein the microwave power density is 1.5-2.0W/cm 3, so that the specific surface area of the biochar is stabilized in the range of 120-150m 2/g. |9. The carbon sequestration and emission reduction paddy field straw returning method according to claim 5, wherein the blockchain carbon sink certificate generation method comprises:| determining delta 13 C value of-28 to-26 per mill by using a laser ablation-isotope mass spectrometry combined technology, and establishing a straw carbon fingerprint database; | deploying HyperledgerFabric-based private chain nodes, wherein each block comprises a time stamp, GPS coordinates and a fixed carbon hash value, and the time stamp error of each block is less than or equal to 1s; | and a zero knowledge proof algorithm is introduced to verify the authenticity of the data, so that the privacy data is ensured not to be revealed during the transaction of the carbon asset. (CN120345407)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of agricultural environmental protection, in particular to a carbon fixation and emission reduction rice field straw returning method.|BACKGROUND ART|[0002] Under the current large background of sustainable development and climate change, reasonable treatment of rice field straw and carbon fixation and emission reduction technology become research hot spots. The traditional rice field straw returning mode has a plurality of defects, and severely restricts the improvement of the agricultural ecological environment and the realization of the carbon emission reduction targets.|[0003] From the perspective of carbon fixation and emission reduction, common straw is directly returned to the field or simply burnt, so that carbon resources in the straw cannot be fully utilized, and a large amount of greenhouse gases can be generated due to insufficient decomposition of the straw. The common returning mode lacks scientific regulation and control on straw treatment and microorganism utilization, so that the methane emission is large, the carbon fixation efficiency is extremely low, and the ever-increasing carbon emission reduction requirement worldwide is difficult to meet.|[0004] In terms of soil improvement, it is difficult to effectively improve the soil structure by conventional methods. Simple straw turning and burying cannot form an ideal pore structure, the air permeability, the water retention and the fertilizer retention of soil cannot be obviously improved, even the nutrient balance of the soil is possibly influenced slowly due to straw decomposition, the growth and development of crop root systems are not facilitated, and the crop yield and quality are further influenced.|[0005] For farmland management and carbon metering, the traditional mode relies on manual experience, and a real-time and accurate monitoring and regulating means is lacked. Key indexes such as Eh value, CH 4 concentration and microbial activity of soil cannot be mastered in time, irrigation and fertilization strategies are difficult to adjust according to actual conditions of the soil, and resource waste and environmental pollution are caused. Meanwhile, in the fields of carbon metering and carbon transaction, a scientific, accurate and traceable metering method and a data management system are lacked, reliable basis cannot be provided for carbon asset transaction, and healthy development of an agricultural carbon transaction market is hindered.|[0006] In view of the above, the existing rice field straw returning technology has obvious shortcomings in carbon fixation and emission reduction, soil improvement, accurate management, carbon metering and the like, and an innovative method for solving the problems is urgently needed to realize green sustainable development of agriculture.|DISCLOSURE|Disclosure of Invention|[0007] Technical problem to be solved|[0008] Aiming at the defects existing in the prior art, the invention provides a carbon-fixing and emission-reducing rice field straw returning method, which can efficiently fix carbon and reduce emission through straw pretreatment, biochar preparation and fungus-carbon coupling returning; the three-layer stubble burying structure is matched with humic acid, improves the soil structure, improves the ventilation, water and fertilizer retention performance of the soil structure, is beneficial to crop growth, realizes accurate management by means of sensor monitoring and neural network regulation and control, performs carbon metering by combining isotope labeling with blockchain, has accurate and safe data, and provides powerful support for carbon transaction and the like.|[0009] Technical proposal|[0010] In order to achieve the above purpose, the invention is realized by the following technical scheme:|[0011] A carbon fixation and emission reduction rice field straw returning method comprises the following steps: |[0012] S1, straw multistage crushing and pretreatment, namely finishing rice harvesting by adopting a double-knife roller differential harvesting and crushing integrated machine, longitudinally cutting by a front knife roller to form a straw section of 5-8cm, and transversely kneading by a rear knife roller to ensure that the fiber cracking degree is more than or equal to 85 percent and the crushing uniformity variation coefficient is less than or equal to 10 percent; |[0013] S2, gradient activation preparation of biological carbon, namely mixing the straw obtained in the step S1 with a red mud catalyst according to the doping amount of 5-8%, and carrying out three-stage gradient pyrolysis under a mixed atmosphere with the volume ratio of CO 2 to N 2 of 1:3, wherein the three-stage gradient pyrolysis is specifically 200 ℃ per 30min to 400 ℃ per 1h to 550 ℃ per 2h, so as to generate the magnetic biological carbon with the specific surface area of more than or equal to 120m 2/g and the pore size distribution of a micropore and mesopore composite structure, wherein micropores are less than 2nm, mesopores are 2-50nm, and the Fe 3O4 load amount in the magnetic biological carbon is 3-5%; |[0014] S3, bacteria-carbon coupling returning, namely fixing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria in the pores of the biochar according to the proportion of 1:2, and applying a biochar-bacteria complex according to the proportion of 20-30% of the dry weight of the straw, wherein the survival rate of bacteria is more than or equal to 90%/30 days; |[0015] S4, three-dimensional stubble burying and soil improvement, namely, constructing a three-layer stubble burying structure by adopting a hydraulic turnover plow and a rotary cultivator to perform combined operation, wherein the three-layer stubble burying structure comprises a biological carbon mixed layer with the surface layer of 0-10cm, a straw-bacterial agent composite layer with the middle layer of 10-25cm and a red mud solidified layer with the bottom layer of 25-40cm, and a humic acid binder is applied in a matched manner to form a honeycomb pore structure; |[0016] S5, intelligent regulation and carbon metering, namely, deploying a sensor array for LoRa communication, monitoring the Eh value, CH 4 concentration and microbial activity of the soil in real time, dynamically adjusting an irrigation strategy and the activation frequency of a microbial inoculum through a convolutional neural network, and synchronously tracking the carbon flow direction of the straw by using delta 13C isotope labeling and generating a blockchain carbon sink voucher. |[0017] Further, the red mud catalyst in the step S2 is required to be modified by hydrochloric acid with the concentration of 0.5mol/L, wherein the solid-liquid ratio is 1:5, the specific surface area is increased to 150m 2/g, the magnetic load realizes the Fe 2+/Fe3 + mol ratio of 1:2 by a coprecipitation method, and the strength of an external magnetic field is 0.5T.|[0018] Furthermore, the immobilization of the microbial inoculum adopts a sodium alginate-biochar composite gel embedding technology, the matching degree of pore size distribution and the size of the microbial cells is more than or equal to 90 percent, and a micro-aerobic environment is constructed to maintain the activity of methane-oxidizing bacteria, wherein the dissolved oxygen in the micro-aerobic environment is 0.5-1.5mg/L.|[0019] Still further, the intelligent regulation and control system includes:|[0020] the multispectral unmanned aerial vehicle collects the NDVI index and the thermal infrared image of the paddy field every week, and a three-dimensional emission model is built; |[0021] The edge computing gateway runs an LSTM neural network model, wherein the prediction precision R 2 is more than or equal to 0.92; |[0022] The response time of the water valve driven by the piezoelectric ceramic and the electric control microbial inoculum atomizing nozzle is less than or equal to 50ms, and the diameter of fog drops of the electric control microbial inoculum atomizing nozzle is 50-80 mu m. |[0023] Further, a region adaptation model is established:|[0024] in a damp-heat climate zone, the red mud doping amount is increased to 10 percent, and ventilation concealed pipes are arranged, wherein the distance between the ventilation concealed pipes is 1.5m; |[0025] in the saline-alkali area, the porosity of the biochar is improved by 40% through modification of 1 mol/LNaOH. |[0026] Still further, full lifecycle management includes:|[0027] The UHFRFID label is adopted in the straw collection stage to track the water content and the heat value; |[0028] A microwave energy monitoring system is deployed in the biochar production stage, wherein the standing wave ratio is less than or equal to 1.5; |[0029] the carbon sink data generates a tamper-proof credential through HyperledgerFabric architecture. |[0030] Furthermore, the compound microbial inoculum in the step S3 adopts a sodium alginate-biochar compound gel embedding technology, and specifically comprises the following steps:|[0031] Mixing magnetic biochar with sodium alginate solution according to a mass ratio of 1:3 to form a gel precursor; |[0032] Gel microspheres with the particle size of 50-200 mu m are prepared by a microfluidic technology, and the matching degree of the pore diameter and the thallus size is more than or equal to 90%; |[0033] the gradient oxygen environment is built in the gel microsphere, specifically, 1.5-2.0mg/L of surface dissolved oxygen, 0.3-0.8mg/L of core dissolved oxygen and 0.5-1.0% humic acid are synchronously loaded as a slow-release nutrition source. |[0034] Furthermore, the biochar preparation process in the step S2 is dynamically regulated and controlled through a machine learning model, and specifically comprises the following steps:|[0035] Constructing an LSTM neural network model, wherein input parameters comprise 8-12% of straw water content, 5-8% of red mud catalyst doping amount and 10-20 ℃ per minute of heating rate; |[0036] Collecting data of the flow rate of mixed gas of CO 2 and N 2 of 0.8-1.2m/s and the specific surface area of a product in real time in the carbonization process, optimizing model parameters through transfer learning, and predicting the accuracy R 2 to be more than or equal to 0.93; |[0037] And dynamically adjusting the microwave power density and the injection rate of the activating agent NH 3 according to the model output, wherein the microwave power density is 1.5-2.0W/cm 3, so that the specific surface area of the biochar is stabilized in the range of 120-150m 2/g. |[0038] Still further, the blockchain carbon sink credential generation method includes:|[0039] The delta 13C value is measured by a laser ablation-isotope mass spectrometry technology and is-28 to-26 per mill, and a straw carbon fingerprint database is established; |[0040] deploying HyperledgerFabric-based private chain nodes, wherein each block comprises a time stamp, GPS coordinates and a fixed carbon hash value, and the time stamp error of each block is less than or equal to 1s; |[0041] and a zero knowledge proof algorithm is introduced to verify the authenticity of the data, so that the privacy data is ensured not to be revealed during the transaction of the carbon asset. |[0042] Advantageous effects|[0043] Compared with the prior art, the technical proposal provided by the invention has the following advantages that|[0044] The beneficial effects are that:|[0045] 1. The invention adopts a three-layer stubble burying structure constructed by the combined operation of the hydraulic turnover plow and the rotary cultivator, a surface biochar mixing layer, a middle straw-microbial inoculum composite layer and a bottom red mud solidifying layer are matched with a humic acid binder to form a honeycomb pore structure, thus enhancing the air permeability, the water retention property and the fertilizer retention property of soil, preventing the bottom layer from leaking by the red mud solidifying layer, optimizing the physical and chemical properties of the soil and creating a good environment for the growth of crops. |[0046] 2. According to the invention, through the multi-stage crushing pretreatment of the straw, the straw fiber cracking degree is more than or equal to 85% and the crushing uniformity variation coefficient is less than or equal to 10%, the magnetic biochar is prepared by subsequent gradient activation, the specific surface area of the generated magnetic biochar is more than or equal to 120m 2/g, and the biochar is coupled with halophilic methane oxidizing bacteria and high-temperature cellulose decomposing bacteria in a specific proportion to return to the field, so that the characteristics of microorganisms and the biochar can be fully utilized, the fixed conversion of straw carbon in soil can be accelerated, methane generation can be inhibited, the carbon emission of a rice field can be effectively reduced, and the carbon fixing capability can be improved.|[0047] 3. According to the invention, the key indexes of soil are monitored in real time by means of the LoRa communication sensor array, the irrigation strategy and the microbial inoculum activation frequency are dynamically adjusted by using the convolutional neural network, so that accurate agricultural management is realized, and the resource utilization efficiency is improved. Meanwhile, the delta 13C isotope labeling is used for tracking the carbon flow direction of the straw, and a block chain technology is combined to generate a tamper-proof carbon sink certificate, so that scientific and accurate carbon metering is ensured, and solid data support and safety guarantee are provided for carbon transaction and carbon asset management.|INVENTION MODE|Detailed Description|[0048] In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be clearly and completely described in the following in conjunction with the embodiments of the present invention. It will be apparent that the described embodiments are some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0049] The invention is further described below with reference to examples.|[0050] Example 1 basic technical solution|[0051] S1, straw multistage crushing and pretreatment|[0052] A double-knife-roller differential harvesting and crushing integrated machine (model: JQ-3000) is adopted for harvesting rice and crushing straw. The front knife roller is longitudinally cut to form straw sections with the length of 6cm, the rear knife roller is transversely subjected to yarn kneading treatment, the fiber cracking degree reaches 87% (. Gtoreq.85%), and the uniformity coefficient of variation of crushing is 8% (. Gtoreq.10%). The water content of the crushed straw is controlled to be 10 percent, and the straw is calibrated in real time by an infrared moisture meter (precision + -0.5 percent). The straw is crushed and then enters the next working procedure within 48 hours so as to prevent the oxidative degradation of the fiber.|[0053] S2, gradient activation preparation of biochar|[0054] Modification of a red mud catalyst:|[0055] mixing red mud and 0.5mol/L hydrochloric acid according to a solid-to-liquid ratio of 1:5, stirring for 2 hours, centrifuging at 3000rpm for 10 minutes, and drying to obtain the modified red mud catalyst, wherein the specific surface area of the modified red mud catalyst is increased to 150m 2/g (the original red mud is 80m 2/g). |[0056] The magnetic loading is realized by a coprecipitation method, namely Fe 2+ and Fe 3+ are mixed according to a molar ratio of 1:2, and the mixture reacts under the condition of an external magnetic field strength of 0.5T to form uniform Fe 3O4 nano particles.|[0057] Mixing and gradient pyrolysis:|[0058] Mixing the straw obtained in the step S1 with the modified red mud according to the doping amount of 6%, and placing the mixture in a mixed atmosphere of CO 2 and N 2 in a volume ratio of 1:3 for three-stage gradient pyrolysis: |[0059] the first stage is 200 ℃ per 30min (volatile organic compounds are removed in the initial stage of pyrolysis, and the heating rate is 10 ℃ per min); |[0060] The second stage is 400 ℃ per 1h (promoting the formation of carbon skeleton, and the microwave power density is 1.5W/cm 3); |[0061] And in the third stage, 550 ℃ per 2h (Fe 3O4 loading reaches 4 percent), and the microwave power density is improved to 2.0W/cm 3. |[0062] Finally preparing the magnetic biochar, wherein the specific surface area is 135m 2/g(≥120m2/g, the pore size distribution is a micropore (< 2 nm) and mesoporous (2-50 nm) composite structure, and the porosity is 45%.|[0063] S3, returning to field by bacterium-carbon coupling|[0064] Embedding a bacterial agent:|[0065] The halophilic methane-oxidizing bacteria (strain No.: methylcoccussp.HY-01) and the high temperature resistant cellulolytic bacteria (strain No.: thermobifidafuscaTF-02) were mixed in a 1:2 ratio. |[0066] The porous ceramic material is fixed in the pores of the biochar by the sodium alginate-biochar composite gel embedding technology:|[0067] the particle size of the gel microsphere is 100 mu m; |[0068] The pore matching degree is 92% (. Gtoreq.90%); |[0069] dissolved oxygen gradient, surface layer 1.8mg/L, core region 0.5mg/L. |[0070] The survival rate of the microbial inoculum is kept 93 percent (more than or equal to 90 percent) within 30 days, and the addition amount of the humic acid sustained release agent is 1.0 percent.|[0071] The proportion of the preparation is that the biochar-fungicide complex is prepared according to 25 percent of the dry weight of the straw and the plant is sowed in a pneumatic type (the sowing uniformity is more than or equal to 95 percent).|[0072] S4, three-dimensional stubble burying and soil improvement|[0073] The hydraulic turnover plow (model: HF-500) and rotary cultivator (model: XG-2000) are adopted to construct a three-layer stubble burying structure:|[0074] The surface layer (0-10 cm) is a biochar mixed layer, and forms a honeycomb pore structure (the porosity is 45%) with humic acid binder (the addition amount is 2 kg/mu), so that the soil air permeability is improved; |[0075] the middle layer (10-25 cm) is a straw-microbial agent composite layer, the density of the straw is 300 kg/mu, and the microbial activity ATP content is more than or equal to 5nmol/g; |[0076] the bottom layer (25-40 cm) is a red mud solidified layer, the red mud doping amount is 8%, the compactness reaches 90%, and the bottom layer is prevented from leaking. |[0077] S5, intelligent regulation and control and carbon metering|[0078] Sensor deployment:|[0079] The LoRa sensor array (model: LS-200) was deployed in a field every 10m x 10m grid, monitored in real time: |[0080] soil Eh value (-150 to +200 mV); |[0081] CH 4 concentration (precision ± 0.1 ppm); |[0082] microbial Activity (ATP detector accuracy.+ -. 0.2 nmol/g). |[0083] Dynamic regulation:|[0084] Sensor data are analyzed through a Convolutional Neural Network (CNN) model, and irrigation water quantity (error is less than or equal to 5%) and parameters of a microbial inoculum atomizing nozzle (the diameter of mist drops is 60 mu m, and the scope of claims is 50-80 mu m) are dynamically adjusted. |[0085] The edge computing gateway (model: ECG-5000) runs the LSTM model (R 2 = 0.94, claim ≡0.92) and predicts CH 4 emission peak time error +.10 min.|[0086] Carbon tracking and credential generation:|[0087] tracking the carbon flow direction of the straw by using a delta 13C isotope labeling technology (delta 13C value-27 per mill); |[0088] The blockchain carbon sink certificate is generated through HyperledgerFabric architecture, each block comprises a time stamp (error is less than or equal to 1 s), GPS coordinates and a fixed carbon amount hash value, and a zero knowledge proof algorithm (ZKP-200 protocol) is introduced to ensure data privacy. |[0089] Example 2 humid and hot climate zone Adaptation scheme|[0090] The following parameters were adjusted on the basis of example 1:|[0091] the mixing amount of the red mud is increased to 10%, and ventilation hidden pipes (the distance is 1.5 m) are arranged at the bottom layer, and PVC materials (the diameter is 50 mm) are adopted to enhance the air permeability of the soil; |[0092] The pyrolysis heating rate is adjusted to 15 ℃ per minute, the pyrolysis period is shortened to 2.5 hours, and the microwave power density is stabilized at 1.8W/cm 3; |[0093] And (3) upgrading an intelligent regulation system: |[0094] the response time of the piezoelectric ceramic driving water valve is optimized to 45ms; |[0095] the multispectral unmanned aerial vehicle (model: MSD-1000) collects NDVI index (resolution 0.1m 2) and thermal infrared images every week, and a three-dimensional emission model (error is less than or equal to 8%) is constructed. |[0096] Example 3 saline-alkali soil Adaptation scheme|[0097] Modifying biochar, namely reacting the biochar with 1mol/LNaOH solution for 24 hours, improving the porosity by 42 percent, and increasing the specific surface area to 145m 2/g;|[0098] the formula of the microbial inoculum is regulated, namely the halophilic bacteria proportion is increased to 1:1, and the dissolved oxygen gradient is regulated to be 2.0mg/L on the surface layer and 0.8mg/L on the core area; |[0099] Carbon metering optimization, namely measuring delta 13C value (error + -0.3 per mill) by using a laser ablation-isotope mass spectrometry combined technology (LA-ICP-MS), and deploying a microwave energy monitoring system (standing wave ratio is less than or equal to 1.5). |[0100] Comparative example|[0101] Comparative example 1 Single temperature pyrolysis|[0102] Step S2 was modified to 550 ℃ single temperature pyrolysis for 3 hours, with the remainder being as in example 1.|[0103] As a result, the specific surface area of the biochar is only 90m 2/g,Fe3O4, the load is uneven (3.2 percent), and the porosity is reduced to 30 percent.|[0104] Comparative example 2 embedding technique without microbial agent|[0105] In the step S3, the microbial inoculum and the biochar are directly mixed, and gel embedding is not adopted.|[0106] As a result, the survival rate of the microbial agent is reduced to 70% after 30 days, the emission reduction rate of CH 4 is reduced by 35%, and the activity retention rate of the microorganism is only 75%.|[0107] Comparative example 3 traditional irrigation management|[0108] And (5) omitting the intelligent regulation and control system in the step (S5) and adopting artificial irrigation and fertilization.|[0109] As a result, the Eh value of the soil fluctuates by +/-50 mV, the microorganism activity retention rate is only 82%, and the CH 4 emission reduction rate is reduced by 58%.|[0110] Comparison table:|[0111] TABLE 1 biochar Performance comparison |[0112] |[0113] Examples 1-3 significantly increased the biochar specific surface area and porosity by gradient pyrolysis and red mud modification, whereas comparative example 1 resulted in reduced performance due to single temperature pyrolysis. The saline-alkali soil adaptation scheme (example 3) further optimizes the pore structure through NaOH modification, and is suitable for a high-salt environment.|[0114] TABLE 2 microbial inoculum Activity and emission reduction Effect|[0115] |[0116] The bacteria-carbon embedding technology of the embodiment 1 ensures the long-acting activity of the bacteria agent, and the emission reduction of CH 4 is improved by 55 percent. The non-embedding of comparative example 2 causes the death of the microbial inoculum, and the emission reduction efficiency is greatly reduced.|[0117] TABLE 3 Intelligent control of System Performance|[0118] |[0119] |[0120] The intelligent regulation and control system of the embodiment 1-2 is remarkably superior to the traditional management (comparative example 3) in irrigation precision and response speed through real-time data optimization, and the carbon tracking error is controlled within 0.5 per mill, so that the carbon transaction authentication requirement is met.|[0121] In summary, in the embodiment 1, carbon fixation efficiency of 2.8tCO 2 e/mu, CH 4 emission reduction of 15.2 kg/mu and microorganism activity retention rate of 95% are realized through gradient pyrolysis, fungus-carbon coupling and intelligent regulation and control technologies, in the embodiment 2, CH 4 peak prediction precision reaches 94% through ventilation and concealed pipes and LSTM model optimization in a hot and humid climate area, carbon sink credential generation efficiency is improved by 20%, in the embodiment 3, porosity and fungus agent proportion are optimized for saline-alkali soil, NDVI index error is less than or equal to 8%, and carbon asset transaction safety is guaranteed through a zero knowledge proof algorithm.|[0122] The foregoing embodiments are merely for illustrating the technical solution of the present invention, but not for limiting the same, and although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those skilled in the art that modifications may be made to the technical solution described in the foregoing embodiments or equivalents may be substituted for parts of the technical features thereof, and such modifications or substitutions may be made without departing from the spirit and scope of the technical solution of the embodiments of the present invention. (CN120345407)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of agricultural environmental protection, in particular to a carbon fixation and emission reduction rice field straw returning method.|BACKGROUND ART|[0002] Under the current large background of sustainable development and climate change, reasonable treatment of rice field straw and carbon fixation and emission reduction technology become research hot spots. The traditional rice field straw returning mode has a plurality of defects, and severely restricts the improvement of the agricultural ecological environment and the realization of the carbon emission reduction targets.|[0003] From the perspective of carbon fixation and emission reduction, common straw is directly returned to the field or simply burnt, so that carbon resources in the straw cannot be fully utilized, and a large amount of greenhouse gases can be generated due to insufficient decomposition of the straw. The common returning mode lacks scientific regulation and control on straw treatment and microorganism utilization, so that the methane emission is large, the carbon fixation efficiency is extremely low, and the ever-increasing carbon emission reduction requirement worldwide is difficult to meet.|[0004] In terms of soil improvement, it is difficult to effectively improve the soil structure by conventional methods. Simple straw turning and burying cannot form an ideal pore structure, the air permeability, the water retention and the fertilizer retention of soil cannot be obviously improved, even the nutrient balance of the soil is possibly influenced slowly due to straw decomposition, the growth and development of crop root systems are not facilitated, and the crop yield and quality are further influenced.|[0005] For farmland management and carbon metering, the traditional mode relies on manual experience, and a real-time and accurate monitoring and regulating means is lacked. Key indexes such as Eh value, CH 4 concentration and microbial activity of soil cannot be mastered in time, irrigation and fertilization strategies are difficult to adjust according to actual conditions of the soil, and resource waste and environmental pollution are caused. Meanwhile, in the fields of carbon metering and carbon transaction, a scientific, accurate and traceable metering method and a data management system are lacked, reliable basis cannot be provided for carbon asset transaction, and healthy development of an agricultural carbon transaction market is hindered.|[0006] In view of the above, the existing rice field straw returning technology has obvious shortcomings in carbon fixation and emission reduction, soil improvement, accurate management, carbon metering and the like, and an innovative method for solving the problems is urgently needed to realize green sustainable development of agriculture.|DISCLOSURE|Disclosure of Invention|[0007] Technical problem to be solved|[0008] Aiming at the defects existing in the prior art, the invention provides a carbon-fixing and emission-reducing rice field straw returning method, which can efficiently fix carbon and reduce emission through straw pretreatment, biochar preparation and fungus-carbon coupling returning; the three-layer stubble burying structure is matched with humic acid, improves the soil structure, improves the ventilation, water and fertilizer retention performance of the soil structure, is beneficial to crop growth, realizes accurate management by means of sensor monitoring and neural network regulation and control, performs carbon metering by combining isotope labeling with blockchain, has accurate and safe data, and provides powerful support for carbon transaction and the like.|[0009] Technical proposal|[0010] In order to achieve the above purpose, the invention is realized by the following technical scheme:|[0011] A carbon fixation and emission reduction rice field straw returning method comprises the following steps: |[0012] S1, straw multistage crushing and pretreatment, namely finishing rice harvesting by adopting a double-knife roller differential harvesting and crushing integrated machine, longitudinally cutting by a front knife roller to form a straw section of 5-8cm, and transversely kneading by a rear knife roller to ensure that the fiber cracking degree is more than or equal to 85 percent and the crushing uniformity variation coefficient is less than or equal to 10 percent; |[0013] S2, gradient activation preparation of biological carbon, namely mixing the straw obtained in the step S1 with a red mud catalyst according to the doping amount of 5-8%, and carrying out three-stage gradient pyrolysis under a mixed atmosphere with the volume ratio of CO 2 to N 2 of 1:3, wherein the three-stage gradient pyrolysis is specifically 200 ℃ per 30min to 400 ℃ per 1h to 550 ℃ per 2h, so as to generate the magnetic biological carbon with the specific surface area of more than or equal to 120m 2/g and the pore size distribution of a micropore and mesopore composite structure, wherein micropores are less than 2nm, mesopores are 2-50nm, and the Fe 3O4 load amount in the magnetic biological carbon is 3-5%; |[0014] S3, bacteria-carbon coupling returning, namely fixing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria in the pores of the biochar according to the proportion of 1:2, and applying a biochar-bacteria complex according to the proportion of 20-30% of the dry weight of the straw, wherein the survival rate of bacteria is more than or equal to 90%/30 days; |[0015] S4, three-dimensional stubble burying and soil improvement, namely, constructing a three-layer stubble burying structure by adopting a hydraulic turnover plow and a rotary cultivator to perform combined operation, wherein the three-layer stubble burying structure comprises a biological carbon mixed layer with the surface layer of 0-10cm, a straw-bacterial agent composite layer with the middle layer of 10-25cm and a red mud solidified layer with the bottom layer of 25-40cm, and a humic acid binder is applied in a matched manner to form a honeycomb pore structure; |[0016] S5, intelligent regulation and carbon metering, namely, deploying a sensor array for LoRa communication, monitoring the Eh value, CH 4 concentration and microbial activity of the soil in real time, dynamically adjusting an irrigation strategy and the activation frequency of a microbial inoculum through a convolutional neural network, and synchronously tracking the carbon flow direction of the straw by using delta 13C isotope labeling and generating a blockchain carbon sink voucher. |[0017] Further, the red mud catalyst in the step S2 is required to be modified by hydrochloric acid with the concentration of 0.5mol/L, wherein the solid-liquid ratio is 1:5, the specific surface area is increased to 150m 2/g, the magnetic load realizes the Fe 2+/Fe3 + mol ratio of 1:2 by a coprecipitation method, and the strength of an external magnetic field is 0.5T.|[0018] Furthermore, the immobilization of the microbial inoculum adopts a sodium alginate-biochar composite gel embedding technology, the matching degree of pore size distribution and the size of the microbial cells is more than or equal to 90 percent, and a micro-aerobic environment is constructed to maintain the activity of methane-oxidizing bacteria, wherein the dissolved oxygen in the micro-aerobic environment is 0.5-1.5mg/L.|[0019] Still further, the intelligent regulation and control system includes:|[0020] the multispectral unmanned aerial vehicle collects the NDVI index and the thermal infrared image of the paddy field every week, and a three-dimensional emission model is built; |[0021] The edge computing gateway runs an LSTM neural network model, wherein the prediction precision R 2 is more than or equal to 0.92; |[0022] The response time of the water valve driven by the piezoelectric ceramic and the electric control microbial inoculum atomizing nozzle is less than or equal to 50ms, and the diameter of fog drops of the electric control microbial inoculum atomizing nozzle is 50-80 mu m. |[0023] Further, a region adaptation model is established:|[0024] in a damp-heat climate zone, the red mud doping amount is increased to 10 percent, and ventilation concealed pipes are arranged, wherein the distance between the ventilation concealed pipes is 1.5m; |[0025] in the saline-alkali area, the porosity of the biochar is improved by 40% through modification of 1 mol/LNaOH. |[0026] Still further, full lifecycle management includes:|[0027] The UHFRFID label is adopted in the straw collection stage to track the water content and the heat value; |[0028] A microwave energy monitoring system is deployed in the biochar production stage, wherein the standing wave ratio is less than or equal to 1.5; |[0029] the carbon sink data generates a tamper-proof credential through HyperledgerFabric architecture. |[0030] Furthermore, the compound microbial inoculum in the step S3 adopts a sodium alginate-biochar compound gel embedding technology, and specifically comprises the following steps:|[0031] Mixing magnetic biochar with sodium alginate solution according to a mass ratio of 1:3 to form a gel precursor; |[0032] Gel microspheres with the particle size of 50-200 mu m are prepared by a microfluidic technology, and the matching degree of the pore diameter and the thallus size is more than or equal to 90%; |[0033] the gradient oxygen environment is built in the gel microsphere, specifically, 1.5-2.0mg/L of surface dissolved oxygen, 0.3-0.8mg/L of core dissolved oxygen and 0.5-1.0% humic acid are synchronously loaded as a slow-release nutrition source. |[0034] Furthermore, the biochar preparation process in the step S2 is dynamically regulated and controlled through a machine learning model, and specifically comprises the following steps:|[0035] Constructing an LSTM neural network model, wherein input parameters comprise 8-12% of straw water content, 5-8% of red mud catalyst doping amount and 10-20 ℃ per minute of heating rate; |[0036] Collecting data of the flow rate of mixed gas of CO 2 and N 2 of 0.8-1.2m/s and the specific surface area of a product in real time in the carbonization process, optimizing model parameters through transfer learning, and predicting the accuracy R 2 to be more than or equal to 0.93; |[0037] And dynamically adjusting the microwave power density and the injection rate of the activating agent NH 3 according to the model output, wherein the microwave power density is 1.5-2.0W/cm 3, so that the specific surface area of the biochar is stabilized in the range of 120-150m 2/g. |[0038] Still further, the blockchain carbon sink credential generation method includes:|[0039] The delta 13C value is measured by a laser ablation-isotope mass spectrometry technology and is-28 to-26 per mill, and a straw carbon fingerprint database is established; |[0040] deploying HyperledgerFabric-based private chain nodes, wherein each block comprises a time stamp, GPS coordinates and a fixed carbon hash value, and the time stamp error of each block is less than or equal to 1s; |[0041] and a zero knowledge proof algorithm is introduced to verify the authenticity of the data, so that the privacy data is ensured not to be revealed during the transaction of the carbon asset. |[0042] Advantageous effects|[0043] Compared with the prior art, the technical proposal provided by the invention has the following advantages that|[0044] The beneficial effects are that:|[0045] 1. The invention adopts a three-layer stubble burying structure constructed by the combined operation of the hydraulic turnover plow and the rotary cultivator, a surface biochar mixing layer, a middle straw-microbial inoculum composite layer and a bottom red mud solidifying layer are matched with a humic acid binder to form a honeycomb pore structure, thus enhancing the air permeability, the water retention property and the fertilizer retention property of soil, preventing the bottom layer from leaking by the red mud solidifying layer, optimizing the physical and chemical properties of the soil and creating a good environment for the growth of crops. |[0046] 2. According to the invention, through the multi-stage crushing pretreatment of the straw, the straw fiber cracking degree is more than or equal to 85% and the crushing uniformity variation coefficient is less than or equal to 10%, the magnetic biochar is prepared by subsequent gradient activation, the specific surface area of the generated magnetic biochar is more than or equal to 120m 2/g, and the biochar is coupled with halophilic methane oxidizing bacteria and high-temperature cellulose decomposing bacteria in a specific proportion to return to the field, so that the characteristics of microorganisms and the biochar can be fully utilized, the fixed conversion of straw carbon in soil can be accelerated, methane generation can be inhibited, the carbon emission of a rice field can be effectively reduced, and the carbon fixing capability can be improved.|[0047] 3. According to the invention, the key indexes of soil are monitored in real time by means of the LoRa communication sensor array, the irrigation strategy and the microbial inoculum activation frequency are dynamically adjusted by using the convolutional neural network, so that accurate agricultural management is realized, and the resource utilization efficiency is improved. Meanwhile, the delta 13C isotope labeling is used for tracking the carbon flow direction of the straw, and a block chain technology is combined to generate a tamper-proof carbon sink certificate, so that scientific and accurate carbon metering is ensured, and solid data support and safety guarantee are provided for carbon transaction and carbon asset management.|INVENTION MODE|Detailed Description|[0048] In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be clearly and completely described in the following in conjunction with the embodiments of the present invention. It will be apparent that the described embodiments are some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0049] The invention is further described below with reference to examples.|[0050] Example 1 basic technical solution|[0051] S1, straw multistage crushing and pretreatment|[0052] A double-knife-roller differential harvesting and crushing integrated machine (model: JQ-3000) is adopted for harvesting rice and crushing straw. The front knife roller is longitudinally cut to form straw sections with the length of 6cm, the rear knife roller is transversely subjected to yarn kneading treatment, the fiber cracking degree reaches 87% (. Gtoreq.85%), and the uniformity coefficient of variation of crushing is 8% (. Gtoreq.10%). The water content of the crushed straw is controlled to be 10 percent, and the straw is calibrated in real time by an infrared moisture meter (precision + -0.5 percent). The straw is crushed and then enters the next working procedure within 48 hours so as to prevent the oxidative degradation of the fiber.|[0053] S2, gradient activation preparation of biochar|[0054] Modification of a red mud catalyst:|[0055] mixing red mud and 0.5mol/L hydrochloric acid according to a solid-to-liquid ratio of 1:5, stirring for 2 hours, centrifuging at 3000rpm for 10 minutes, and drying to obtain the modified red mud catalyst, wherein the specific surface area of the modified red mud catalyst is increased to 150m 2/g (the original red mud is 80m 2/g). |[0056] The magnetic loading is realized by a coprecipitation method, namely Fe 2+ and Fe 3+ are mixed according to a molar ratio of 1:2, and the mixture reacts under the condition of an external magnetic field strength of 0.5T to form uniform Fe 3O4 nano particles.|[0057] Mixing and gradient pyrolysis:|[0058] Mixing the straw obtained in the step S1 with the modified red mud according to the doping amount of 6%, and placing the mixture in a mixed atmosphere of CO 2 and N 2 in a volume ratio of 1:3 for three-stage gradient pyrolysis: |[0059] the first stage is 200 ℃ per 30min (volatile organic compounds are removed in the initial stage of pyrolysis, and the heating rate is 10 ℃ per min); |[0060] The second stage is 400 ℃ per 1h (promoting the formation of carbon skeleton, and the microwave power density is 1.5W/cm 3); |[0061] And in the third stage, 550 ℃ per 2h (Fe 3O4 loading reaches 4 percent), and the microwave power density is improved to 2.0W/cm 3. |[0062] Finally preparing the magnetic biochar, wherein the specific surface area is 135m 2/g(≥120m2/g, the pore size distribution is a micropore (< 2 nm) and mesoporous (2-50 nm) composite structure, and the porosity is 45%.|[0063] S3, returning to field by bacterium-carbon coupling|[0064] Embedding a bacterial agent:|[0065] The halophilic methane-oxidizing bacteria (strain No.: methylcoccussp.HY-01) and the high temperature resistant cellulolytic bacteria (strain No.: thermobifidafuscaTF-02) were mixed in a 1:2 ratio. |[0066] The porous ceramic material is fixed in the pores of the biochar by the sodium alginate-biochar composite gel embedding technology:|[0067] the particle size of the gel microsphere is 100 mu m; |[0068] The pore matching degree is 92% (. Gtoreq.90%); |[0069] dissolved oxygen gradient, surface layer 1.8mg/L, core region 0.5mg/L. |[0070] The survival rate of the microbial inoculum is kept 93 percent (more than or equal to 90 percent) within 30 days, and the addition amount of the humic acid sustained release agent is 1.0 percent.|[0071] The proportion of the preparation is that the biochar-fungicide complex is prepared according to 25 percent of the dry weight of the straw and the plant is sowed in a pneumatic type (the sowing uniformity is more than or equal to 95 percent).|[0072] S4, three-dimensional stubble burying and soil improvement|[0073] The hydraulic turnover plow (model: HF-500) and rotary cultivator (model: XG-2000) are adopted to construct a three-layer stubble burying structure:|[0074] The surface layer (0-10 cm) is a biochar mixed layer, and forms a honeycomb pore structure (the porosity is 45%) with humic acid binder (the addition amount is 2 kg/mu), so that the soil air permeability is improved; |[0075] the middle layer (10-25 cm) is a straw-microbial agent composite layer, the density of the straw is 300 kg/mu, and the microbial activity ATP content is more than or equal to 5nmol/g; |[0076] the bottom layer (25-40 cm) is a red mud solidified layer, the red mud doping amount is 8%, the compactness reaches 90%, and the bottom layer is prevented from leaking. |[0077] S5, intelligent regulation and control and carbon metering|[0078] Sensor deployment:|[0079] The LoRa sensor array (model: LS-200) was deployed in a field every 10m x 10m grid, monitored in real time: |[0080] soil Eh value (-150 to +200 mV); |[0081] CH 4 concentration (precision ± 0.1 ppm); |[0082] microbial Activity (ATP detector accuracy.+ -. 0.2 nmol/g). |[0083] Dynamic regulation:|[0084] Sensor data are analyzed through a Convolutional Neural Network (CNN) model, and irrigation water quantity (error is less than or equal to 5%) and parameters of a microbial inoculum atomizing nozzle (the diameter of mist drops is 60 mu m, and the scope of claims is 50-80 mu m) are dynamically adjusted. |[0085] The edge computing gateway (model: ECG-5000) runs the LSTM model (R 2 = 0.94, claim ≡0.92) and predicts CH 4 emission peak time error +.10 min.|[0086] Carbon tracking and credential generation:|[0087] tracking the carbon flow direction of the straw by using a delta 13C isotope labeling technology (delta 13C value-27 per mill); |[0088] The blockchain carbon sink certificate is generated through HyperledgerFabric architecture, each block comprises a time stamp (error is less than or equal to 1 s), GPS coordinates and a fixed carbon amount hash value, and a zero knowledge proof algorithm (ZKP-200 protocol) is introduced to ensure data privacy. |[0089] Example 2 humid and hot climate zone Adaptation scheme|[0090] The following parameters were adjusted on the basis of example 1:|[0091] the mixing amount of the red mud is increased to 10%, and ventilation hidden pipes (the distance is 1.5 m) are arranged at the bottom layer, and PVC materials (the diameter is 50 mm) are adopted to enhance the air permeability of the soil; |[0092] The pyrolysis heating rate is adjusted to 15 ℃ per minute, the pyrolysis period is shortened to 2.5 hours, and the microwave power density is stabilized at 1.8W/cm 3; |[0093] And (3) upgrading an intelligent regulation system: |[0094] the response time of the piezoelectric ceramic driving water valve is optimized to 45ms; |[0095] the multispectral unmanned aerial vehicle (model: MSD-1000) collects NDVI index (resolution 0.1m 2) and thermal infrared images every week, and a three-dimensional emission model (error is less than or equal to 8%) is constructed. |[0096] Example 3 saline-alkali soil Adaptation scheme|[0097] Modifying biochar, namely reacting the biochar with 1mol/LNaOH solution for 24 hours, improving the porosity by 42 percent, and increasing the specific surface area to 145m 2/g;|[0098] the formula of the microbial inoculum is regulated, namely the halophilic bacteria proportion is increased to 1:1, and the dissolved oxygen gradient is regulated to be 2.0mg/L on the surface layer and 0.8mg/L on the core area; |[0099] Carbon metering optimization, namely measuring delta 13C value (error + -0.3 per mill) by using a laser ablation-isotope mass spectrometry combined technology (LA-ICP-MS), and deploying a microwave energy monitoring system (standing wave ratio is less than or equal to 1.5). |[0100] Comparative example|[0101] Comparative example 1 Single temperature pyrolysis|[0102] Step S2 was modified to 550 ℃ single temperature pyrolysis for 3 hours, with the remainder being as in example 1.|[0103] As a result, the specific surface area of the biochar is only 90m 2/g,Fe3O4, the load is uneven (3.2 percent), and the porosity is reduced to 30 percent.|[0104] Comparative example 2 embedding technique without microbial agent|[0105] In the step S3, the microbial inoculum and the biochar are directly mixed, and gel embedding is not adopted.|[0106] As a result, the survival rate of the microbial agent is reduced to 70% after 30 days, the emission reduction rate of CH 4 is reduced by 35%, and the activity retention rate of the microorganism is only 75%.|[0107] Comparative example 3 traditional irrigation management|[0108] And (5) omitting the intelligent regulation and control system in the step (S5) and adopting artificial irrigation and fertilization.|[0109] As a result, the Eh value of the soil fluctuates by +/-50 mV, the microorganism activity retention rate is only 82%, and the CH 4 emission reduction rate is reduced by 58%.|[0110] Comparison table:|[0111] TABLE 1 biochar Performance comparison |[0112] |[0113] Examples 1-3 significantly increased the biochar specific surface area and porosity by gradient pyrolysis and red mud modification, whereas comparative example 1 resulted in reduced performance due to single temperature pyrolysis. The saline-alkali soil adaptation scheme (example 3) further optimizes the pore structure through NaOH modification, and is suitable for a high-salt environment.|[0114] TABLE 2 microbial inoculum Activity and emission reduction Effect|[0115] |[0116] The bacteria-carbon embedding technology of the embodiment 1 ensures the long-acting activity of the bacteria agent, and the emission reduction of CH 4 is improved by 55 percent. The non-embedding of comparative example 2 causes the death of the microbial inoculum, and the emission reduction efficiency is greatly reduced.|[0117] TABLE 3 Intelligent control of System Performance|[0118] |[0119] |[0120] The intelligent regulation and control system of the embodiment 1-2 is remarkably superior to the traditional management (comparative example 3) in irrigation precision and response speed through real-time data optimization, and the carbon tracking error is controlled within 0.5 per mill, so that the carbon transaction authentication requirement is met.|[0121] In summary, in the embodiment 1, carbon fixation efficiency of 2.8tCO 2 e/mu, CH 4 emission reduction of 15.2 kg/mu and microorganism activity retention rate of 95% are realized through gradient pyrolysis, fungus-carbon coupling and intelligent regulation and control technologies, in the embodiment 2, CH 4 peak prediction precision reaches 94% through ventilation and concealed pipes and LSTM model optimization in a hot and humid climate area, carbon sink credential generation efficiency is improved by 20%, in the embodiment 3, porosity and fungus agent proportion are optimized for saline-alkali soil, NDVI index error is less than or equal to 8%, and carbon asset transaction safety is guaranteed through a zero knowledge proof algorithm.|[0122] The foregoing embodiments are merely for illustrating the technical solution of the present invention, but not for limiting the same, and although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those skilled in the art that modifications may be made to the technical solution described in the foregoing embodiments or equivalents may be substituted for parts of the technical features thereof, and such modifications or substitutions may be made without departing from the spirit and scope of the technical solution of the embodiments of the present invention. Family Number|(115358899)|115358899|Abstract|(CN120345407B B)|The invention relates to the technical field of agricultural environmental protection , in particular to a carbon sequestration and emission reduction rice field straw returning method , which comprises the following steps : performing multistage crushing pretreatment on straws , mixing with red mud , performing gradient pyrolysis to prepare magnetic biochar , fixing specific strains , returning to the field , constructing a three - layer stubble burying structure to improve soil , and performing sensor monitoring and neural network regulation . And carbon sequestration emission reduction and intelligent management are realized , and the carbon flow direction can be tracked and a carbon sink voucher can be generated . According to the invention , through straw pretreatment , biochar preparation and fungus - carbon coupling returning , efficient carbon sequestration and emission reduction can be realized ; the three - layer stubble burying structure is matched with humic acid , so that the soil structure is improved , the air permeability and water and fertilizer retention performance are improved , and crop growth is facilitated ; by means of sensor monitoring and neural network regulation and control , precise management is achieved , carbon metering is conducted by combining isotope labeling with the block chain , data are accurate and safe , and powerful support is provided for carbon transactions and the like . |CPC codes|(CN120345407B B)|A01B - 033/02/1 |A01B - 033/08 |A01B - 033/10/3 |A01B - 033/12 |A01B - 033/14/2 |A01B - 049/02/7 |A01B - 049/06/5 |A01G - 025/16/7 |IPC codes|(CN120345407B B)|A01B - 033/02 |A01B - 033/08 |A01B - 033/10 |A01B - 033/12 |A01B - 033/14 |A01B - 049/02 |A01B - 049/06 |A01G - 025/16 |Title|(CN120345407 A)|Rice field straw returning method for carbon sequestration and emission reduction | Other special machines A01B-033/02/1|A01B-033/10|A01B-033/10/3|A01B-049/02/2|A01G-025/02|A01G-025/16/7|Y02A-040/238|Y02P-060/23 A01B-033/02/1|A01B-033/10|A01B-033/10/3|A01B-049/02/2|A01G-025/02|A01G-025/16/7|Y02A-040/238|Y02P-060/23 A01B-033/02|A01B-033/08|A01B-033/10|A01B-033/12|A01B-033/14|A01B-049/02|A01B-049/06|A01G-025/16 A01B-033/02|A01B-033/08|A01B-033/10|A01B-033/12|A01B-033/14|A01B-049/02|A01B-049/06|A01G-025/16 CN119896089|US20150232349|KR101017576|CN119344006|CN108941194 CN119896089 114378656 WHO=Examiner SELF=N CAT=A|US20150232349 65078625 WHO=Examiner SELF=N CAT=A|KR101017576 34205034 WHO=Examiner SELF=N CAT=A|CN119344006 113174618 WHO=Examiner SELF=N|CN108941194 82411031 WHO=Examiner SELF=N KR101017576; US20150232349; CN119896089; CN119344006; CN108941194 GRANTED (CN120345407)|GRANTED ALIVE (CN120345407)|ALIVE (CN120345407)|LEGAL DETAILS FOR CN120345407|Actual or expected expiration date=2045-05-20|Legal state=ALIVE|Status=GRANTED|Event publication date=2025-05-20|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510651543|Application date=2025-05-20|Standardized application number=2025CN-0651543|Event publication date=2025-07-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120345407|Publication stage code=A|Publication date=2025-07-22|Standardized publication number=CN120345407|Event publication date=2025-07-22|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-08-08|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-09-02|Event code=CN/CB02|Event group=Change of name or address Reassignment|Change of applicant information|FORMER APPLICANT:AGRICULTURAL AND PASTORAL SCIENCE RES INSTITUTE OF XHINGAN UNION APPLICANT:XINGAN LEAGUE AGRICULTURE AND ANIMAL HUSBANDRY ACAD|Event publication date=2025-11-28|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN120345407|Publication stage code=B|Publication date=2025-11-28|Standardized publication number=CN120345407B|Event publication date=2025-11-28|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN120345407)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKeXcALKV8Ru5hj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000079925408&ekey=2159&xpn=CN120345407B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=Ssam7gLYEFtVYKbPI89S07msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN120345407)|CN|(CN120345407)|CN (CN120345407)|NAME=AGRICULTURAL AND PASTORAL SCIENCE RES INSTITUTE OF XHINGAN UNION , COUNTRY=CN|(CN120345407)|NAME=AGRICULTURAL AND PASTORAL SCIENCE RES INSTITUTE OF XHINGAN UNION , COUNTRY=CN (CN120345407)|NAME=TIAN YUXUAN;SHENZHEN FENG CHENG ZHI HE INTELLECTUAL PROPERTY AGENCY CO. LTD , REG=44525|(CN120345407)|NAME=TIAN YUXUAN;SHENZHEN FENG CHENG ZHI HE INTELLECTUAL PROPERTY AGENCY CO. LTD , REG=44525 (CN120345407)|CN| (CN120345407)|NAME=Xu Xingjian No. 9 Nongyan Lane, Wucha Road, Ulanhot City, Xing'an League, Inner Mongolia Autonomous Region, 137000 Ulanhot City, CITY=Hinggan League, POSTCODE=137000, STATE=The Inner Mongolia Autonomous Region , COUNTRY=CN |NAME=Bai Lu|NAME=Gu Yanru|NAME=Wen Li|NAME=Sun Wurina|NAME=Liang Shuang|NAME=Xue Hainan|NAME=Han Lei|NAME=Liu Jicong|NAME=Liang Yi|NAME=Ning Xiaomeng|NAME=Ma Benchi|NAME=Luo Wei|NAME=Han Feng|(CN120345407)|NAME=XU XINGJIAN|NAME=BAI LU|NAME=GU YANRU|NAME=WEN LI|NAME=SUN WURINA|NAME=LIANG SHUANG|NAME=XUE HAINAN|NAME=HAN LEI|NAME=LIU JICONG|NAME=LIANG YI|NAME=NING XIAOMENG|NAME=MA BENCHI|NAME=LUO WEI|NAME=HAN FENG 0 1 Titre: (CN120345407)|Rice field straw returning method for carbon fixation and emission reduction Résumé: (CN120345407)|The invention relates to the technical field of agricultural environmental protection, in particular to a carbon sequestration and emission reduction rice field straw returning method, which comprises the following steps: performing multistage crushing pretreatment on straws, mixing with red mud, performing gradient pyrolysis to prepare magnetic biochar, fixing specific strains, returning to the field, constructing a three-layer stubble burying structure to improve soil, and performing sensor monitoring and neural network regulation. And carbon sequestration emission reduction and intelligent management are realized, and the carbon flow direction can be tracked and a carbon sink voucher can be generated. According to the invention, through straw pretreatment, biochar preparation and fungus-carbon coupling returning, efficient carbon sequestration and emission reduction can be realized; the three-layer stubble burying structure is matched with humic acid, so that the soil structure is improved, the air permeability and water and fertilizer retention performance are improved, and crop growth is facilitated; by means of sensor monitoring and neural network regulation and control, precise management is achieved, carbon metering is conducted by combining isotope labeling with the block chain, data are accurate and safe, and powerful support is provided for carbon transactions and the like. 4 Abstract gpt-4o-mini no The article focuses on a method for carbon sequestration using agricultural practices and biochar, without addressing the accelerated weathering of minerals or CO₂ capture through mineral carbonation.
4 CN202411180530 CN202411180530 CN119288600|CN119288600 113022604 CN119288600 B 2025-12-12 [CN119288600B]|CN119288600 A 2025-01-10 [CN119288600] 2024-08-27 2024-08-27 2025-12-12|2025-01-10 (CN119288600B)|2025-12-12 (CN119288600)|2044-08-27 (CN119288600)|Carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic ore deposit (CN119288600)|The invention discloses a carbon sequestration filling method based on coal-aluminum symbiotic deposit synchronous mining, and belongs to the technical field of mining. The method comprises the following steps: S1, synchronously mining lower-layer aluminum ore and upper-layer coal mine; s2, coal gangue generated by coal mining is crushed to serve as filling aggregate; s3, performing carbon sequestration and dealkalization treatment on the red mud generated by aluminum ore smelting to be used as a filling cementing material; s4, mixing the two treated solid wastes, and matching cement to meet the relevant national standard of the filling material; and S5, pumping to a coal mine and aluminum mine goaf through a pipeline system to realize carbon sequestration filling. TAIYUAN UNIVERSITY OF TECHNOLOGY (CN119288600)|TAIYUAN UNIVERSITY OF TECHNOLOGY ([CN])|(CN119288600)|TAIYUAN UNIVERSITY OF TECHNOLOGY ([CN]) FENG GUORUI|WU GUOWEI|BAI JINWEN|HAN YANNA|MA JUNBIAO|LI XIRAN|SU SHENGYU|WU FAN (CN119288600)|FENG GUORUI|WU GUOWEI|BAI JINWEN|HAN YANNA|MA JUNBIAO|LI XIRAN|SU SHENGYU|WU FAN|(CN119288600)|FENG GUORUI|WU GUOWEI|BAI JINWEN|HAN YANNA|MA JUNBIAO|LI XIRAN|SU SHENGYU|WU FAN (CN119288600)|SHEN YANLING;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY|Reg. Nb: 14101 (CN119288600)|The coal-aluminum resource mining efficiency of the enterprise is improved by more than 20% by the carbon-fixing filling method based on the coal-aluminum symbiotic ore deposit synchronous mining, the red mud and coal gangue solid waste treatment cost is saved for the enterprise by about 200 ten thousand, the effect of fixing 30 kg of CO _2 per ton of red mud in the red mud dealkalization process is realized, and the problems of surface subsidence and groundwater resource damage caused by underground mining are solved.| (CN119288600)|1. The carbon fixation filling method based on synchronous mining of the coal-aluminum symbiotic deposit is characterized by comprising the following steps of: s1, coal and aluminum synchronous mining, namely, aluminum ore at the lower layer and coal mine at the upper layer are synchronously mined, wherein the mined aluminum ore is subjected to aluminum smelting by a Bayer process to obtain Bayer process red mud, and the mined coal mine is subjected to separation and coal washing to obtain coal gangue; S2, gangue treatment, namely crushing and screening the separated gangue to ensure that the granularity of the gangue meets the requirement of filling aggregate; s3, carbon fixation and dealkalization treatment of the red mud, namely introducing CO 2 gas with purity of more than 99% into the Bayer process red mud, and dealkalizing to meet the requirements of filling materials; in the red mud treatment method, CO 2 gas is introduced into the red mud to carry out dealkalization treatment, and the pH value of the Bayer process red mud is reduced to 6.5-8.5 through acid-base neutralization reaction, so that the pH value requirement of red mud landfill is met; S4, adding cement into the two treated solid wastes, mixing the two treated solid wastes according to the ratio of red mud to coal gangue to cement=2-4:2-4, adding water to adjust the solid-to-liquid ratio to be 0.6-1.0, and stirring to prepare a filling material, wherein the obtained filling material meets the requirement that the uniaxial compressive strength is 2.5-10 MPa and the slump is more than 10mm; s5, pumping the filling material to the coal mine and aluminum mine goaf for filling through a pipeline pumping system, arranging a pipeline system in the same filling well, arranging a coal seam goaf filling pipeline and an aluminum mine layer goaf filling pipeline, wherein the pipeline system extends from a ground filling pump station to the coal seam and aluminum mine layer goaf all the way, conveying the filling material through the coal seam goaf filling pipeline to fill the upper coal seam goaf, and conveying the filling material through the aluminum mine layer goaf filling pipeline to fill the lower aluminum mine layer goaf; And in the pipeline pumping system, a steel pipe with the pipe diameter of 20cm is used for slurry filling, the pumping pressure is 1.5MPa, the filling material is pumped to the goaf of the coal mine and the aluminum mine, and carbon fixation filling is implemented. | (CN119288600)|The invention discloses a carbon fixing and filling method based on synchronous mining of coal-aluminum symbiotic deposits, and belongs to the technical field of mining.|The invention provides a carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic ore deposits, which comprises the following process steps:|The invention relates to a carbon fixing and filling method based on synchronous mining of coal-aluminum symbiotic deposits, and belongs to the technical field of mining.| (CN119288600)|CARBON FIXATION(100,16)|SYNCHRONOUS MINING(100,14)|COAL ALUMINUM SYMBIOTIC ORE(100,1)|COAL ALUMINUM SYMBIOTIC DEPOSIT(64,9)|COAL GANGUE(61,18)|PIPELINE PUMPING(47,5)|CRUSHING COAL GANGUE(46,1)|DEALKALIZATION TREATMENT(45,9)|ORE DEPOSIT SYNCHRONOUS MINING(44,1)|GANGUE GRANULARITY(42,3)|PIPELINE(35,23)|ALUMINUM MINE LAYER(33,4)|COAL MINE GOAF(33,4)|RED MUD SEQUESTRATION(33,2)|ORE DEPOSIT SYNCHRONOUS EXPLOITATION(33,1)|FILLING AGGREGATE(32,4)|DEALKALIZATION PLANT(32,3)|COAL MINE(31,13)|ALUMINUM SYNCHRONOUS MINING(31,3)|FILLING AGGREGATE REQUIREMENT(31,3)|MINED COAL MINE(31,3)|CEMENT PROPORTION(31,1)|RED MUD LANDFILL REQUIREMENT(30,3)|FILLING SLURRY PREPARATION PLANT(30,2)|RED MUD DEALKALIZATION TREATMENT(29,3)|RED MUD(28,50)|UNIAXIAL COMPRESSIVE STRENGTH(28,8)|COAL SEAM GOAF(28,4)|ENTERPRISE(28,2)|GROUNDWATER RESOURCE DAMAGE(28,1)|ROOF SINKING(28,1)|COAL ALUMINUM ORE ENTERPRISE(26,1)|COAL GANGUE SOLID WASTE(26,1)|COAL SORTING(26,1)|RED MUD TON(26,1)|ORE DEPOSIT(24,9)|RED MUD LANDFILL(24,3)|COAL ALUMINUM RESOURCE(24,1)|COAL ALUMINUM SYNCHRONOUS MINING(24,1)|ALUMINUM ORE MINING(23,3)|MINING(23,2)|SEPARATED GANGUE(22,7)|GANGUE TREATMENT(22,3)|ALUMINUM MINE(21,4)|CARBON FIXATION FILLING(21,4)|COMPACT GOAF(21,1)|SLURRY FILLING(19,5)|MIXING TREATED COAL GANGUE(19,3)|BROKEN GANGUE(19,1)|UNDERGROUND MINING(19,1)|ALUMINUM ORE(18,9)|RED MUD TREATMENT(18,6)|SLUMP(18,6)|CEMENT ADDITION(18,3)|COAL SEAM(17,9)|DEALKALIZED RED MUD(17,3)|RED MUD DEALKALIZATION(16,1)|FILLING ROOF(15,3)|RED MUD PROPORTION(15,3)|ALUMINUM ORE SMELTING(15,2)|RED MUD RATIO(15,2)|LAND FILLING PUMP STATION(14,4)|FILLING MATERIAL(13,17)|BAYER PROCESS RED MUD(13,15)|CARBON FIXING(13,10)|DEALKALIZATION WORKSHOP(13,5)|DENSE FILLING(13,3)|RELEVANT NATIONAL STANDARD(13,1)|COMPRESSIVE STRENGTH(12,9)|FILLING SLURRY PREPARATION WORKSHOP(11,5)|CARBON SEQUESTRATION(11,4)|UPPER COAL SEAM(11,4)|COAL WASHING(11,3)|NEUTRALIZATION REACTION(11,2)|BAYER(10,19)|PIPE DIAMETER(10,6)|ALUMINUM SMELTING(10,5)|PUMPING PRESSURE(10,5)|PURITY(10,4)|SAFETY PRODUCTION(10,2)|SURFACE SUBSIDENCE(10,1)|COAL(9,8)|FILLING MATERIAL REQUIREMENT(9,3)|FILLING MATERIAL MEET(9,2)|GOAF FILLING PIPELINE(9,2)|BREAKING(9,1)|ALUMINUM MINERAL SEAM(8,4)|ALUMINUM ORE LAYER(7,9)|UPPER COAL LAYER(7,2)|COAL GANGUE TRANSPORTATION(7,1)|STEEL PIPE(6,7)|UPPER LAYER(6,3)|ACID BASE NEUTRALIZATION REACTION(6,2)|CRUSHED GANGUE(6,2)|COAL ALUMINUM AFFILIATED ENTERPRISE(6,1)|TREATMENT COST(6,1)|UPPER LAYER COAL MINE(6,1)|COAL BED(5,2)|ALUMINUM SEAM GOAF(5,1)|ALUMINUM SYNCHRONOUS EXPLOITATION(5,1)|COAL EXPLOITATION(5,1)|COAL MINE SYNCHRONOUS FILLING(5,1)|STOPE ROCK STABILITY(5,1)|SOLID WASTE(4,5)|FILLING WELL(4,4)|PARTICLE SIZE(4,4)|ALUMINUM SMELTING PLANT(4,2)|COAL ALUMINUM COOCCURRENCE DEPOSIT(4,1)|COAL SEAM EXPLOITATION(4,1)|COAL SEAM HORIZON RELATION(4,1)|FILLING COMPACTION(4,1)|FILLING GOAF(4,1)|FILLING SLURRY CONVEYING(4,1)|LANDFILL REQUIREMENT(4,1)|MINING COAL MINE(4,1)|RED MUD CARBON FIXING(3,5)|SOLID LIQUID RATIO(3,3)|ACID BASE(3,2)|CEMENTING MATERIAL(3,2)|COAL WASHERY(3,2)|CRUSHING(3,2)|LAYER GOAF(3,2)|SINKING(3,2)|ALUMINUM FACTORY(3,1)|ALUMINUM ORE ENTERPRISE(3,1)|ALUMINUM SMELTING FACTORY(3,1)|CEMENT CONSUMPTION(3,1)|COAL MINE WASHING(3,1)|MINING PRODUCTION SAFETY(3,1)|NEARBY SEPARATION(3,1)|SLURRY PREPARATION PLANT(3,1)||(CN119288600)|CARBON FIXATION(100,17)|SYNCHRONOUS MINING(100,17)|COAL ALUMINUM SYMBIOTIC DEPOSIT(100,10)|SYMBIOTIC DEPOSIT(100,10)|COAL ALUMINUM SYMBIOTIC ORE(100,1)|SYMBIOTIC ORE(100,1)|COAL GANGUE(69,23)|SYMBIOTIC ORE DEPOSIT(56,9)|COAL ALUMINUM SYMBIOTIC ORE DEPOSIT(54,9)|SYMBIOTIC DEPOSIT SYNCHRONOUS MINING(43,1)|CRUSHING COAL GANGUE(42,1)|GANGUE GRANULARITY(39,3)|BAUXITE SMELTING(38,1)|CRUSHED COAL GANGUE(38,1)|PIPELINE PUMPING(35,5)|DEALKALIZATION WORKSHOP(33,7)|DEALKALIZATION TREATMENT(32,8)|COAL MINE GOAF(31,4)|FILLING AGGREGATE(30,4)|COAL MINE(29,14)|MINED COAL MINE(29,3)|ALUMINUM SYNCHRONOUS MINING(28,3)|FILLING AGGREGATE REQUIREMENT(28,3)|CEMENT PROPORTION(28,1)|RED MUD(27,58)|FILLING SLURRY PREPARATION WORKSHOP(27,7)|UNIAXIAL COMPRESSIVE STRENGTH(26,8)|RED MUD DEALKALIZATION TREATMENT(26,3)|GROUNDWATER RESOURCE DAMAGE(26,1)|ROOF SINKING(26,1)|ENTERPRISE(25,2)|COAL SORTING(24,1)|COAL ALUMINUM ORE ENTERPRISE(23,1)|COAL GANGUE SOLID WASTE(23,1)|RED MUD TON(23,1)|COAL ALUMINUM SYNCHRONOUS MINING(22,1)|ALUMINUM ORE MINING(21,3)|MINING(21,2)|COAL ALUMINUM RESOURCE(21,1)|SEPARATED COAL GANGUE(21,1)|GANGUE TREATMENT(20,3)|ALUMINUM MINE(19,4)|COMPACT GOAF(19,1)|PIPELINE FILLING(19,1)|MIXING TREATED COAL GANGUE(18,3)|RED MUD LANDFILL REQUIREMENT(18,3)|ALUMINUM ORE(17,9)|SLURRY FILLING(17,6)|CEMENT ADDITION(17,3)|FILLING DRILLING(17,1)|UNDERGROUND MINING(17,1)|SEPARATED GANGUE(16,6)|SLUMP(16,6)|DEALKALIZED RED MUD(15,3)|FILLING ROOF(14,3)|RED MUD CARBON FIXATION(14,3)|CARBON SEQUESTRATION FILLING(14,1)|COAL MINING(14,1)|RED MUD DEALKALIZATION(14,1)|UPPER COAL SEAM GOAF(14,1)|RED MUD PROPORTION(13,3)|ALUMINUM ORE SMELTING(13,2)|RED MUD RATIO(13,2)|ALUMINUM ORE LAYER GOAF(13,1)|CARBON FIXING(12,11)|DENSE FILLING(12,3)|BAYER PROCESS RED MUD(11,15)|COMPRESSIVE STRENGTH(11,9)|RELEVANT NATIONAL STANDARD(11,1)|FILLING MATERIAL(10,16)|PIPE DIAMETER(10,7)|PUMPING PRESSURE(10,6)|CARBON FIXATION FILLING(10,3)|COAL WASHING(10,3)|ALUMINUM SMELTING(9,5)|PURITY(9,4)|SAFETY PRODUCTION(9,2)|ORE DEPOSIT(9,1)|BAYER(8,19)|COAL(8,9)|RED MUD TREATMENT(8,5)|ALUMINUM MINERAL SEAM(8,4)|LAND FILLING PUMP STATION(8,4)|FILLING MATERIAL REQUIREMENT(8,3)|FILLING MATERIAL MEET(8,2)|GOAF FILLING PIPELINE(8,2)|SURFACE SUBSIDENCE(7,2)|COAL GANGUE TRANSPORTATION(7,1)|UPPER LAYER(6,3)|UPPER COAL LAYER(6,2)|STEEL PIPE(5,8)|CRUSHED GANGUE(5,2)|COAL BED HORIZON RELATION(5,1)|TREATMENT COST(5,1)|UPPER LAYER COAL MINE(5,1)|SOLID WASTE(4,5)|PARTICLE SIZE(4,4)|RED MUD DISPOSAL(4,2)|ALUMINUM SEAM GOAF(4,1)|ALUMINUM SYNCHRONOUS EXPLOITATION(4,1)|COAL ALUMINUM COOCCURRENCE DEPOSIT(4,1)|COAL EXPLOITATION(4,1)|COAL MINE SYNCHRONOUS FILLING(4,1)|COAL SEAM EXPLOITATION(4,1)|COAL SHORTAGE(4,1)|DEALKALIZATION PLANT(4,1)|FILLING COMPACTION(4,1)|FILLING GOAF(4,1)|FILLING SLURRY CONVEYING(4,1)|MINING COAL MINE(4,1)|STOPE ROCK STABILITY(4,1)|UNDERGROUND GOAF(4,1)|UNDERGROUND INFILTRATION(4,1)|RED MUD CARBON FIXING(3,5)|ACID BASE NEUTRALIZATION REACTION(3,2)|ALUMINUM SMELTING PLANT(3,2)|CEMENTING MATERIAL(3,2)|ALUMINUM SMELTING FACTORY(3,1)|CEMENT CONSUMPTION(3,1)|COAL MINE WASHING(3,1)|MINING PRODUCTION SAFETY(3,1)|NEARBY SEPARATION(3,1)|OCCUPIED STATE(3,1)|RED MUD HARM(3,1)|SLURRY PREPARATION PLANT(3,1)|SOLID LIQUID RATIO(2,3)|COAL WASHERY(2,2)|CRUSHING(2,2)|ENVIRONMENTAL POLLUTION(2,2)|SINKING(2,2)|ALUMINUM FACTORY(2,1)|ALUMINUM ORE ENTERPRISE(2,1)|ALUMINUM RESOURCE(2,1)|BAYER RED MUD(2,1)|COAL ALUMINUM ENTERPRISE(2,1)| (CN119288600)|1. The carbon fixation filling method based on synchronous mining of the coal-aluminum symbiotic deposit is characterized by comprising the following steps of:| s1, coal and aluminum synchronous mining, namely, aluminum ore at the lower layer and coal mine at the upper layer are synchronously mined, wherein the mined aluminum ore is subjected to aluminum smelting by a Bayer process to obtain Bayer process red mud, and the mined coal mine is subjected to separation and coal washing to obtain coal gangue; | S2, gangue treatment, namely crushing and screening the separated gangue to ensure that the granularity of the gangue meets the requirement of filling aggregate; | s3, carbon fixation and dealkalization treatment of the red mud, namely introducing CO 2 gas with purity of more than 99% into the Bayer process red mud, and dealkalizing to meet the requirements of filling materials; | in the red mud treatment method, CO 2 gas is introduced into the red mud to carry out dealkalization treatment, and the pH value of the Bayer process red mud is reduced to 6.5-8.5 through acid-base neutralization reaction, so that the pH value requirement of red mud landfill is met; | S4, adding cement into the two treated solid wastes, mixing the two treated solid wastes according to the ratio of red mud to coal gangue to cement=2-4:2-4, adding water to adjust the solid-to-liquid ratio to be 0.6-1.0, and stirring to prepare a filling material, wherein the obtained filling material meets the requirement that the uniaxial compressive strength is 2.5-10 MPa and the slump is more than 10mm; | s5, pumping the filling material to the coal mine and aluminum mine goaf for filling through a pipeline pumping system, arranging a pipeline system in the same filling well, arranging a coal seam goaf filling pipeline and an aluminum mine layer goaf filling pipeline, wherein the pipeline system extends from a ground filling pump station to the coal seam and aluminum mine layer goaf all the way, conveying the filling material through the coal seam goaf filling pipeline to fill the upper coal seam goaf, and conveying the filling material through the aluminum mine layer goaf filling pipeline to fill the lower aluminum mine layer goaf; | And in the pipeline pumping system, a steel pipe with the pipe diameter of 20cm is used for slurry filling, the pumping pressure is 1.5MPa, the filling material is pumped to the goaf of the coal mine and the aluminum mine, and carbon fixation filling is implemented. |2. The carbon fixation filling method based on synchronous mining of the coal-aluminum symbiotic deposit of claim 1 is characterized in that S1 coal-aluminum synchronous mining is that an upper coal layer and a lower aluminum ore layer are synchronously mined under the condition that safety production and related standards are met, and a coal-aluminum ore enterprise has the conditions of near smelting of aluminum ore and near sorting of coal, so that further processing and transportation of Bayer process red mud and coal gangue obtained later are facilitated.|3. The carbon sequestration filling method based on synchronous mining of coal-aluminum symbiotic deposits of claim 1, wherein the coal gangue in S2 is crushed and sorted into particles with the particle size smaller than 20mm, and the mass ratio of the particles with the particle size smaller than 5mm is 30% -50%.|4. The carbon-fixing filling method based on synchronous mining of coal-aluminum symbiotic ore deposit of claim 1 wherein S4 is formed by mixing treated coal gangue and treated red mud, cement is added, the optimal proportion of the red mud to the coal gangue to the cement=4:2:4 is adopted, water is added to adjust the solid-liquid ratio to be 0.8, the uniaxial compressive strength is 7.8MPa, and the slump is 13cm.|5. The carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic ore deposit of claim 1 is characterized in that a full filling mode is adopted until a compact goaf is reached, the volume weight of a compact filling body is 2g/cm 3, the actual uniaxial compressive strength is more than 7.0MPa, the filling roof grafting rate is more than 90%, and the roof sinking amount is relieved by more than 85%.|6. The carbon sequestration filling method based on coal-aluminum symbiotic ore deposit synchronous exploitation according to claim 1, wherein a gangue breaking plant, a red mud sequestration dealkalization plant and a filling slurry preparation plant are arranged on the ground above the ore deposit, separated gangue is transported to the gangue breaking plant for breaking, bayer process red mud is transported to the red mud sequestration dealkalization plant for dealkalization treatment, and then the broken gangue and dealkalized red mud are mixed in the filling slurry preparation plant, and cement and water are added to prepare the filling material. (CN119288600)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to a carbon fixing and filling method based on synchronous mining of coal-aluminum symbiotic deposits, and belongs to the technical field of mining.|BACKGROUND ART|[0002] When alumina is industrially prepared, a large amount of solid waste red mud is generated, and 1.0-1.8 t of red mud is discharged every 1t of alumina is produced due to the different production processes of aluminum factories. The red mud produced by the Bayer process accounts for more than 90% of the total discharge of the red mud.|[0003] The gangue is solid waste discharged in the coal exploitation and washing process, and compared with common coal, the gangue has the characteristics of low carbon content, low heat value and hard texture, and is one of mine solid waste.|[0004] Goaf filling can ensure the production safety of mining and increase the surrounding rock stability of stopes, but the cost problem of filling materials and the problem of filling slurry conveying are the constraint factors of technological development, and the significance of fully utilizing coal gangue generated by mining coal mines and red mud generated by aluminum smelting to prepare the filling materials meeting the related working performance and economic benefit is great.|[0005] The alkaline characteristic of the red mud is fully considered, the cement consumption is reduced by utilizing the solid waste, and meanwhile, the method of absorbing CO 2 by the red mud in alkaline is expected to realize the clean zero emission of carbon and even negative emission for coal-aluminum enterprises.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to solve a series of problems caused by stacking of red mud and coal gangue, and provides a carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic deposits.|[0007] According to the method, two bulk solid wastes of red mud and coal gangue can be utilized in a large scale, and the upper-layer aluminum ore and the lower-layer coal mine can be simultaneously and safely and efficiently mined in a synchronous filling mode.|[0008] The invention provides a carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic ore deposits, which comprises the following process steps:|[0009] s1, coal and aluminum synchronous mining, namely, aluminum ore at the lower layer and coal mine at the upper layer are synchronously mined, wherein the mined aluminum ore is subjected to aluminum smelting by a Bayer process to obtain Bayer process red mud, and the mined coal mine is subjected to separation and coal washing to obtain coal gangue; |[0010] S2, gangue treatment, namely crushing and screening the separated gangue to ensure that the granularity of the gangue meets the requirement of filling aggregate; |[0011] s3, carbon fixation and dealkalization treatment of the red mud, namely introducing CO 2 gas with purity of more than 99% into the Bayer process red mud, and dealkalizing to meet the requirements of filling materials; |[0012] S4, adding cement into the two treated solid wastes, mixing and preparing a filling material by adding water to adjust the solid-liquid ratio to be 0.6-1.0 (mass ratio) according to the ratio of red mud to gangue to cement=2-4:2-4, wherein the obtained filling material meets the requirement that the uniaxial compressive strength is 2.5-10 MPa and the slump is more than 10mm; |[0013] and S5, pumping the filling material to the goaf of the coal mine and the aluminum mine for filling through a pipeline pumping system. |[0014] Further, in S1, the coal and aluminum synchronous exploitation is that the upper coal layer and the lower aluminum ore layer are synchronously exploited under the condition that the safety production and related standards are met, and the coal and aluminum ore enterprises have the condition that aluminum ores are smelted nearby, so that the further treatment and transportation of the Bayer process red mud obtained later are convenient, and meanwhile, the nearby separation condition of coal is provided, and the further treatment and transportation of coal gangue are also convenient.|[0015] Further, the gangue in the S2 is treated by crushing and sorting the gangue into particles with the particle size smaller than 20mm, and the mass ratio of the particles with the particle size smaller than 5mm is 30% -50%.|[0016] Further, in the S3, CO 2 gas is introduced into the red mud for dealkalization treatment, and the pH value of the Bayer process red mud is reduced to be within the range of 6.5-8.5 through acid-base neutralization reaction, so that the pH value requirement of red mud landfill is met.|[0017] Further, S4 is formed by mixing treated coal gangue and treated red mud, cement is added, the optimal proportion of the red mud to the coal gangue to the cement=4:2:4 is adopted, water is added to adjust the solid-liquid ratio to be 0.8, the uniaxial compressive strength is 7.8MPa, and the slump is 13cm.|[0018] And in the pipeline pumping system in the step S5, a steel pipe with the pipe diameter of 20cm is selected for slurry filling, the pumping pressure is 1.5MPa, the filling material is pumped to a coal mine goaf and an aluminum mine goaf for carbon fixation filling, and the full filling mode is adopted until the goaf is compacted, the volume weight of a compacted filling body is about 2g/cm 3, the actual uniaxial compressive strength is more than 7.0MPa, the filling roof grafting rate is more than 90%, and the sinking amount of a top plate is relieved by more than 85%.|[0019] According to the method, a gangue crushing workshop, a red mud carbon-fixing dealkalization workshop and a filling slurry preparation workshop are arranged on the ground above a mineral deposit, separated gangue is conveyed to the gangue crushing workshop to be crushed, bayer red mud is conveyed to the red mud carbon-fixing dealkalization workshop to be dealkalized, crushed gangue and dealkalized red mud are mixed in the filling slurry preparation workshop, cement and water are added to prepare filling materials, a pipeline system is arranged in a filling well, a coal seam goaf filling pipeline and an aluminum seam goaf filling pipeline are arranged, the pipeline system extends from a ground filling pump station to a coal seam and an aluminum seam goaf all the way, a steel pipe with the pipe diameter of 20cm is selected for slurry filling, pumping pressure is 1.5MPa, the filling materials are conveyed through the coal seam goaf filling pipeline to fill the upper coal seam goaf, and meanwhile, the filling materials are conveyed through the aluminum seam goaf filling pipeline to fill the lower aluminum seam goaf.|[0020] The invention has the beneficial effects that:|[0021] (1) The invention ensures safe and efficient synchronous mining of the coal-aluminum symbiotic ore deposit through synchronous filling of the coal mine and the aluminum mine goaf. |[0022] (2) According to the invention, two solid wastes of red mud generated in aluminum smelting and coal gangue generated in coal mine washing are fully utilized, so that the environmental pollution and safety problems caused by stacking of the red mud and the coal gangue are reduced.|[0023] (3) According to the invention, CO 2 is introduced in the red mud treatment process to dealkalize the red mud, so that the pH value of the red mud can meet the landfill requirement, and the red mud can be used as a cementing material to permanently seal CO 2 underground.|DRAWINGS DESCRIPTION|[0024] FIG. 1 is a schematic diagram of simultaneous mining and carbon sequestration filling of coal-aluminum co-occurrence deposits;|[0025] FIG. 2 is a schematic diagram of coal-aluminum seam locations of a coal-aluminum symbiotic deposit; |[0026] FIG. 3 is a schematic diagram of the effects of simultaneous mining, carbon sequestration and filling of coal-aluminum symbiotic deposits; |[0027] FIG. 4 is a flow chart of the synchronous mining and carbon fixing filling of the coal-aluminum symbiotic deposit; |[0028] in the figure, the coal bed, the aluminum ore layer and the red mud are 1-coal bed, the aluminum ore layer and the aluminum ore layer are 2-coal gangue breaking plant, the red mud carbon fixing and dealkalization plant is 4-red mud, the slurry preparation plant is 5-filled, the well is 6-filled, the goaf filling pipeline of the coal bed is 7-the goaf, the goaf filling pipeline of the aluminum ore layer is 8-the goaf, the filling body is 9-the filling body, the coal washery is 10-the aluminum smelting plant is 11-the aluminum smelting plant. |INVENTION MODE|Detailed Description|[0029] The present invention is further illustrated by, but not limited to, the following examples.|[0030] The invention provides a carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic ore deposits, which comprises the following process steps:|[0031] s1, coal and aluminum synchronous mining, namely, aluminum ore at the lower layer and coal mine at the upper layer are synchronously mined, wherein the mined aluminum ore is subjected to aluminum smelting by a Bayer process to obtain Bayer process red mud, and the mined coal mine is subjected to separation and coal washing to obtain coal gangue; |[0032] S2, gangue treatment, namely crushing and screening the separated gangue to ensure that the granularity of the gangue meets the requirement of filling aggregate; |[0033] s3, carbon fixation and dealkalization treatment of the red mud, namely introducing CO 2 gas with purity of more than 99% into the Bayer process red mud, and dealkalizing to meet the requirements of filling materials; |[0034] S4, mixing two treated solid wastes with additional cement, wherein S4 is formed by mixing treated coal gangue and treated red mud, the additional cement is added according to the optimal proportion of red mud to coal gangue to cement=4:2:4, water is added to adjust the solid-to-liquid ratio to 0.8, the uniaxial compressive strength is 7.8MPa, and the slump is 13cm; |[0035] S5, through a pipeline pumping system, a steel pipe with the pipe diameter of 20cm is selected for slurry filling, the pumping pressure is 1.5MPa, the filling material is pumped to the goaf of the coal mine and the aluminum mine, carbon fixation filling is implemented, and a full filling mode is adopted until the goaf is compact. |[0036] In the method, a gangue crushing workshop 3, a red mud carbon-fixing dealkalization workshop 4 and a filling slurry preparation workshop 5 are arranged on the ground above a mineral deposit, separated gangue is transported to the gangue crushing workshop for crushing, bayer process red mud is transported to the red mud carbon-fixing dealkalization workshop for dealkalization treatment, crushed gangue and dealkalized red mud are mixed in the filling slurry preparation workshop, cement and water are added to prepare filling materials, a pipeline system is arranged in a filling well 6, a coal seam goaf filling pipeline 7 and an aluminum mineral seam goaf filling pipeline 8 are arranged, the pipeline system extends from a ground filling pump station to a coal seam and an aluminum mineral seam goaf, a steel pipe with the pipe diameter of 20cm is selected for slurry filling, pumping pressure is 1.5MPa, the filling materials are transported through the coal seam goaf filling pipeline for filling the goaf, and meanwhile, the filling materials are transported through the aluminum mineral seam goaf filling pipeline 8 for filling the goaf of the lower aluminum mineral seam 2.|[0037] For a clearer understanding of technical objects, features and effects of the present invention, a method for synchronously mining carbon-fixing and filling coal-aluminum symbiotic ore deposit will be described in further detail with reference to the accompanying drawings.|[0038] The horizon relation of the coal seam and the aluminum ore layer of a certain coal-aluminum affiliated enterprise in Lv Liangshi of Shanxi province is shown as 1 and 2 in the figure, the coal thickness of the upper coal seam is 3m, the upper coal seam is a near-horizontal coal seam, the near-horizontal aluminum ore layer with the lower thickness of 2 meters is synchronously mined, and the interlayer spacing between the coal seam and the aluminum ore layer is 50m. Coal is separated in a coal washery 10 positioned in the surface industrial square after coal seam exploitation to obtain coal gangue, and bauxite is subjected to an aluminum smelting factory 11 in the surface industrial square to obtain Bayer process red mud. And (3) conveying the separated gangue to a gangue crushing workshop 3, and crushing the gangue into standard particles with the granularity smaller than 20mm and the particle proportion smaller than 5mm of 30% -50% for standby. The Bayer process red mud is transported to a red mud carbon fixation dealkalization workshop 4, and dealkalization treatment is carried out on the Bayer process red mud by introducing CO 2 with the purity of 99 percent, and the pH value is reduced to 7.5, so that the pH value requirement of red mud landfill is met. And then mixing the treated coal gangue with the treated red mud in a filling slurry preparation workshop 5, adding cement, adding water to adjust the solid-to-liquid ratio to be 0.8 according to the mass ratio of the red mud to the coal gangue to the cement=4:2:4, and stirring to prepare a filling material, wherein the single-axis compressive strength of the obtained filling material is 7.8MPa, and the slump is 13mm. And arranging a pipeline system in the filling well 6, wherein the pipeline system extends from a ground filling pump station to an aluminum mining layer goaf of a coal mine, performing slurry filling by using a steel pipe with the pipe diameter of 20cm, and pumping the steel pipe under the pumping pressure of 1.5MPa, wherein 7 is a coal seam goaf filling pipeline for filling an upper coal seam goaf, 8 is an aluminum mining layer goaf filling pipeline for filling a lower aluminum mining layer goaf, and filling the goaf as much as possible through pumping to form a compact filling body 9. The volume weight of the compact filling body is about 2g/cm 3, the actual uniaxial compressive strength is 7.6MPa, the filling roof grafting rate is 90%, and the sinking amount of the top plate is relieved by more than 85%.|[0039] The coal-aluminum resource mining efficiency of the enterprise is improved by more than 20% by the carbon-fixing filling method based on the coal-aluminum symbiotic ore deposit synchronous mining, the red mud and coal gangue solid waste treatment cost is saved for the enterprise by about 200 ten thousand, the effect of fixing 30 kg of CO 2 per ton of red mud in the red mud dealkalization process is realized, and the problems of surface subsidence and groundwater resource damage caused by underground mining are solved. (CN119288600)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to a carbon fixing and filling method based on synchronous mining of coal-aluminum symbiotic deposits, and belongs to the technical field of mining.|BACKGROUND ART|[0002] When alumina is industrially prepared, a large amount of solid waste red mud is generated, and 1.0-1.8 t of red mud is discharged every 1t of alumina is produced due to the different production processes of aluminum factories. The red mud produced by the Bayer process accounts for more than 90% of the total discharge of the red mud.|[0003] The gangue is solid waste discharged in the coal exploitation and washing process, and compared with common coal, the gangue has the characteristics of low carbon content, low heat value and hard texture, and is one of mine solid waste.|[0004] Goaf filling can ensure the production safety of mining and increase the surrounding rock stability of stopes, but the cost problem of filling materials and the problem of filling slurry conveying are the constraint factors of technological development, and the significance of fully utilizing coal gangue generated by mining coal mines and red mud generated by aluminum smelting to prepare the filling materials meeting the related working performance and economic benefit is great.|[0005] The alkaline characteristic of the red mud is fully considered, the cement consumption is reduced by utilizing the solid waste, and meanwhile, the method of absorbing CO 2 by the red mud in alkaline is expected to realize the clean zero emission of carbon and even negative emission for coal-aluminum enterprises.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to solve a series of problems caused by stacking of red mud and coal gangue, and provides a carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic deposits.|[0007] According to the method, two bulk solid wastes of red mud and coal gangue can be utilized in a large scale, and the upper-layer aluminum ore and the lower-layer coal mine can be simultaneously and safely and efficiently mined in a synchronous filling mode.|[0008] The invention provides a carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic ore deposits, which comprises the following process steps:|[0009] s1, coal and aluminum synchronous mining, namely, aluminum ore at the lower layer and coal mine at the upper layer are synchronously mined, wherein the mined aluminum ore is subjected to aluminum smelting by a Bayer process to obtain Bayer process red mud, and the mined coal mine is subjected to separation and coal washing to obtain coal gangue; |[0010] S2, gangue treatment, namely crushing and screening the separated gangue to ensure that the granularity of the gangue meets the requirement of filling aggregate; |[0011] s3, carbon fixation and dealkalization treatment of the red mud, namely introducing CO 2 gas with purity of more than 99% into the Bayer process red mud, and dealkalizing to meet the requirements of filling materials; |[0012] S4, adding cement into the two treated solid wastes, mixing and preparing a filling material by adding water to adjust the solid-liquid ratio to be 0.6-1.0 (mass ratio) according to the ratio of red mud to gangue to cement=2-4:2-4, wherein the obtained filling material meets the requirement that the uniaxial compressive strength is 2.5-10 MPa and the slump is more than 10mm; |[0013] and S5, pumping the filling material to the goaf of the coal mine and the aluminum mine for filling through a pipeline pumping system. |[0014] Further, in S1, the coal and aluminum synchronous exploitation is that the upper coal layer and the lower aluminum ore layer are synchronously exploited under the condition that the safety production and related standards are met, and the coal and aluminum ore enterprises have the condition that aluminum ores are smelted nearby, so that the further treatment and transportation of the Bayer process red mud obtained later are convenient, and meanwhile, the nearby separation condition of coal is provided, and the further treatment and transportation of coal gangue are also convenient.|[0015] Further, the gangue in the S2 is treated by crushing and sorting the gangue into particles with the particle size smaller than 20mm, and the mass ratio of the particles with the particle size smaller than 5mm is 30% -50%.|[0016] Further, in the S3, CO 2 gas is introduced into the red mud for dealkalization treatment, and the pH value of the Bayer process red mud is reduced to be within the range of 6.5-8.5 through acid-base neutralization reaction, so that the pH value requirement of red mud landfill is met.|[0017] Further, S4 is formed by mixing treated coal gangue and treated red mud, cement is added, the optimal proportion of the red mud to the coal gangue to the cement=4:2:4 is adopted, water is added to adjust the solid-liquid ratio to be 0.8, the uniaxial compressive strength is 7.8MPa, and the slump is 13cm.|[0018] And in the pipeline pumping system in the step S5, a steel pipe with the pipe diameter of 20cm is selected for slurry filling, the pumping pressure is 1.5MPa, the filling material is pumped to a coal mine goaf and an aluminum mine goaf for carbon fixation filling, and the full filling mode is adopted until the goaf is compacted, the volume weight of a compacted filling body is about 2g/cm 3, the actual uniaxial compressive strength is more than 7.0MPa, the filling roof grafting rate is more than 90%, and the sinking amount of a top plate is relieved by more than 85%.|[0019] According to the method, a gangue crushing workshop, a red mud carbon-fixing dealkalization workshop and a filling slurry preparation workshop are arranged on the ground above a mineral deposit, separated gangue is conveyed to the gangue crushing workshop to be crushed, bayer red mud is conveyed to the red mud carbon-fixing dealkalization workshop to be dealkalized, crushed gangue and dealkalized red mud are mixed in the filling slurry preparation workshop, cement and water are added to prepare filling materials, a pipeline system is arranged in a filling well, a coal seam goaf filling pipeline and an aluminum seam goaf filling pipeline are arranged, the pipeline system extends from a ground filling pump station to a coal seam and an aluminum seam goaf all the way, a steel pipe with the pipe diameter of 20cm is selected for slurry filling, pumping pressure is 1.5MPa, the filling materials are conveyed through the coal seam goaf filling pipeline to fill the upper coal seam goaf, and meanwhile, the filling materials are conveyed through the aluminum seam goaf filling pipeline to fill the lower aluminum seam goaf.|[0020] The invention has the beneficial effects that:|[0021] (1) The invention ensures safe and efficient synchronous mining of the coal-aluminum symbiotic ore deposit through synchronous filling of the coal mine and the aluminum mine goaf. |[0022] (2) According to the invention, two solid wastes of red mud generated in aluminum smelting and coal gangue generated in coal mine washing are fully utilized, so that the environmental pollution and safety problems caused by stacking of the red mud and the coal gangue are reduced.|[0023] (3) According to the invention, CO 2 is introduced in the red mud treatment process to dealkalize the red mud, so that the pH value of the red mud can meet the landfill requirement, and the red mud can be used as a cementing material to permanently seal CO 2 underground.|DRAWINGS DESCRIPTION|[0024] FIG. 1 is a schematic diagram of simultaneous mining and carbon sequestration filling of coal-aluminum co-occurrence deposits;|[0025] FIG. 2 is a schematic diagram of coal-aluminum seam locations of a coal-aluminum symbiotic deposit; |[0026] FIG. 3 is a schematic diagram of the effects of simultaneous mining, carbon sequestration and filling of coal-aluminum symbiotic deposits; |[0027] FIG. 4 is a flow chart of the synchronous mining and carbon fixing filling of the coal-aluminum symbiotic deposit; |[0028] in the figure, the coal bed, the aluminum ore layer and the red mud are 1-coal bed, the aluminum ore layer and the aluminum ore layer are 2-coal gangue breaking plant, the red mud carbon fixing and dealkalization plant is 4-red mud, the slurry preparation plant is 5-filled, the well is 6-filled, the goaf filling pipeline of the coal bed is 7-the goaf, the goaf filling pipeline of the aluminum ore layer is 8-the goaf, the filling body is 9-the filling body, the coal washery is 10-the aluminum smelting plant is 11-the aluminum smelting plant. |INVENTION MODE|Detailed Description|[0029] The present invention is further illustrated by, but not limited to, the following examples.|[0030] The invention provides a carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic ore deposits, which comprises the following process steps:|[0031] s1, coal and aluminum synchronous mining, namely, aluminum ore at the lower layer and coal mine at the upper layer are synchronously mined, wherein the mined aluminum ore is subjected to aluminum smelting by a Bayer process to obtain Bayer process red mud, and the mined coal mine is subjected to separation and coal washing to obtain coal gangue; |[0032] S2, gangue treatment, namely crushing and screening the separated gangue to ensure that the granularity of the gangue meets the requirement of filling aggregate; |[0033] s3, carbon fixation and dealkalization treatment of the red mud, namely introducing CO 2 gas with purity of more than 99% into the Bayer process red mud, and dealkalizing to meet the requirements of filling materials; |[0034] S4, mixing two treated solid wastes with additional cement, wherein S4 is formed by mixing treated coal gangue and treated red mud, the additional cement is added according to the optimal proportion of red mud to coal gangue to cement=4:2:4, water is added to adjust the solid-to-liquid ratio to 0.8, the uniaxial compressive strength is 7.8MPa, and the slump is 13cm; |[0035] S5, through a pipeline pumping system, a steel pipe with the pipe diameter of 20cm is selected for slurry filling, the pumping pressure is 1.5MPa, the filling material is pumped to the goaf of the coal mine and the aluminum mine, carbon fixation filling is implemented, and a full filling mode is adopted until the goaf is compact. |[0036] In the method, a gangue crushing workshop 3, a red mud carbon-fixing dealkalization workshop 4 and a filling slurry preparation workshop 5 are arranged on the ground above a mineral deposit, separated gangue is transported to the gangue crushing workshop for crushing, bayer process red mud is transported to the red mud carbon-fixing dealkalization workshop for dealkalization treatment, crushed gangue and dealkalized red mud are mixed in the filling slurry preparation workshop, cement and water are added to prepare filling materials, a pipeline system is arranged in a filling well 6, a coal seam goaf filling pipeline 7 and an aluminum mineral seam goaf filling pipeline 8 are arranged, the pipeline system extends from a ground filling pump station to a coal seam and an aluminum mineral seam goaf, a steel pipe with the pipe diameter of 20cm is selected for slurry filling, pumping pressure is 1.5MPa, the filling materials are transported through the coal seam goaf filling pipeline for filling the goaf, and meanwhile, the filling materials are transported through the aluminum mineral seam goaf filling pipeline 8 for filling the goaf of the lower aluminum mineral seam 2.|[0037] For a clearer understanding of technical objects, features and effects of the present invention, a method for synchronously mining carbon-fixing and filling coal-aluminum symbiotic ore deposit will be described in further detail with reference to the accompanying drawings.|[0038] The horizon relation of the coal seam and the aluminum ore layer of a certain coal-aluminum affiliated enterprise in Lv Liangshi of Shanxi province is shown as 1 and 2 in the figure, the coal thickness of the upper coal seam is 3m, the upper coal seam is a near-horizontal coal seam, the near-horizontal aluminum ore layer with the lower thickness of 2 meters is synchronously mined, and the interlayer spacing between the coal seam and the aluminum ore layer is 50m. Coal is separated in a coal washery 10 positioned in the surface industrial square after coal seam exploitation to obtain coal gangue, and bauxite is subjected to an aluminum smelting factory 11 in the surface industrial square to obtain Bayer process red mud. And (3) conveying the separated gangue to a gangue crushing workshop 3, and crushing the gangue into standard particles with the granularity smaller than 20mm and the particle proportion smaller than 5mm of 30% -50% for standby. The Bayer process red mud is transported to a red mud carbon fixation dealkalization workshop 4, and dealkalization treatment is carried out on the Bayer process red mud by introducing CO 2 with the purity of 99 percent, and the pH value is reduced to 7.5, so that the pH value requirement of red mud landfill is met. And then mixing the treated coal gangue with the treated red mud in a filling slurry preparation workshop 5, adding cement, adding water to adjust the solid-to-liquid ratio to be 0.8 according to the mass ratio of the red mud to the coal gangue to the cement=4:2:4, and stirring to prepare a filling material, wherein the single-axis compressive strength of the obtained filling material is 7.8MPa, and the slump is 13mm. And arranging a pipeline system in the filling well 6, wherein the pipeline system extends from a ground filling pump station to an aluminum mining layer goaf of a coal mine, performing slurry filling by using a steel pipe with the pipe diameter of 20cm, and pumping the steel pipe under the pumping pressure of 1.5MPa, wherein 7 is a coal seam goaf filling pipeline for filling an upper coal seam goaf, 8 is an aluminum mining layer goaf filling pipeline for filling a lower aluminum mining layer goaf, and filling the goaf as much as possible through pumping to form a compact filling body 9. The volume weight of the compact filling body is about 2g/cm 3, the actual uniaxial compressive strength is 7.6MPa, the filling roof grafting rate is 90%, and the sinking amount of the top plate is relieved by more than 85%.|[0039] The coal-aluminum resource mining efficiency of the enterprise is improved by more than 20% by the carbon-fixing filling method based on the coal-aluminum symbiotic ore deposit synchronous mining, the red mud and coal gangue solid waste treatment cost is saved for the enterprise by about 200 ten thousand, the effect of fixing 30 kg of CO 2 per ton of red mud in the red mud dealkalization process is realized, and the problems of surface subsidence and groundwater resource damage caused by underground mining are solved. Family Number|(113022604)|113022604|Abstract|(CN119288600B B)|The invention discloses a carbon sequestration filling method based on coal - aluminum symbiotic deposit synchronous mining , and belongs to the technical field of mining . The method comprises the following steps : S1 , synchronously mining lower - layer aluminum ore and upper - layer coal mine ; s2 , coal gangue generated by coal mining is crushed to serve as filling aggregate ; s3 , performing carbon sequestration and dealkalization treatment on the red mud generated by aluminum ore smelting to be used as a filling cementing material ; s4 , mixing the two treated solid wastes , and matching cement to meet the relevant national standard of the filling material ; and S5 , pumping to a coal mine and aluminum mine goaf through a pipeline system to realize carbon sequestration filling . |CPC codes|(CN119288600B B)|B01D - 053/62 |B01D - 053/81 |B01D - 2257/504 |IPC codes|(CN119288600B B)|B01D - 053/62 |B01D - 053/81 |Title|(CN119288600 A)|Carbon sequestration filling method based on synchronous mining of coal - aluminum symbiotic deposit | Civil engineering|Environmental technology|Materials, metallurgy B01D-053/62|B01D-053/81|B01D-2257/504|C04B-007/147|C04B-014/06|C04B-018/04/09|C04B-018/08|C04B-018/12|C04B-018/14/1|C04B-018/16|C04B-020/02/3|C04B-020/02/6|C04B-022/00/2|C04B-022/06/4|C04B-022/12/4|C04B-024/00|C04B-028/00|C04B-028/04|C04B-028/14/3|C04B-028/14/4|C04B-2111/00724|C04B-2111/00767|C04B-2201/50|C05D-001/02|E21C-041/18|E21C-041/22|E21F-015/00|E21F-015/00/5|E21F-015/06|Y02W-030/91|Y02W-030/92|Y02W-030/93|Y02W-030/94|Y02W-030/95 (GR1) C04B-028/00[RK1]; C04B-018/12[RK2]; C04B-018/04/09[RK3]|(GR2) C04B-020/02/3[RK1]; C04B-018/04/09[RK2] B01D-053/62|B01D-053/81|B01D-2257/504|C04B-007/147|C04B-014/06|C04B-018/04/09|C04B-018/08|C04B-018/12|C04B-018/14/1|C04B-018/16|C04B-020/02/3|C04B-020/02/6|C04B-022/00/2|C04B-022/06/4|C04B-022/12/4|C04B-024/00|C04B-028/00|C04B-028/04|C04B-028/14/3|C04B-028/14/4|C04B-2111/00724|C04B-2111/00767|C04B-2201/50|C05D-001/02|E21C-041/18|E21C-041/22|E21F-015/00|E21F-015/00/5|E21F-015/06|Y02W-030/91|Y02W-030/92|Y02W-030/93|Y02W-030/94|Y02W-030/95 B01D-053/62|B01D-053/81|C04B-018/04|C04B-018/12|C04B-020/02|C04B-028/00|E21C-041/18|E21C-041/22|E21F-015/00 B01D-053/62|B01D-053/81|C04B-018/04|C04B-018/12|C04B-020/02|C04B-028/00|E21C-041/18|E21C-041/22|E21F-015/00 CN120211857|CN119860262B CN120211857 115061844 WHO=Examiner SELF=N CAT=A|CN119860262B 114282629 WHO=Examiner SELF=Y CN118065968|CN117449856|CN115263303|CN113292305|CN113061011|CN112707690|US20210040850|CN106278131|US20080179253|CN118187861|CN115321890 CN118065968 109888847 WHO=Examiner SELF=N CAT=A|CN117449856 108295684 WHO=Examiner SELF=N CAT=A|CN115263303 102386976 WHO=Examiner SELF=N CAT=A|CN113292305 95798109 WHO=Examiner SELF=N CAT=A|CN113061011 95030545 WHO=Examiner SELF=N CAT=A|CN112707690 93792531 WHO=Examiner SELF=N CAT=A|US20210040850 83450500 WHO=Examiner SELF=N CAT=A|CN106278131 75046858 WHO=Examiner SELF=Y CAT=A|US20080179253 5187506 WHO=Examiner SELF=N CAT=A|CN118187861 110208643 WHO=Examiner SELF=Y|CN115321890 102539468 WHO=Examiner SELF=N 陈蛟龙;张娜;李恒;赵喜彬;刘晓明;: &quot;赤泥基似膏体充填材料水化特性研究&quot;, 工程科学学报, no. 11, 15 November 2017 (2017-11-15), pages 37 - 43 (Cat. A) US20080179253; CN106278131; CN112707690; CN113061011; CN113292305; CN118065968; US20210040850; CN115263303; CN117449856; CN118187861; CN115321890 GRANTED (CN119288600)|GRANTED ALIVE (CN119288600)|ALIVE (CN119288600)|LEGAL DETAILS FOR CN119288600|Actual or expected expiration date=2044-08-27|Legal state=ALIVE|Status=GRANTED|Event publication date=2024-08-27|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202411180530|Application date=2024-08-27|Standardized application number=2024CN-1180530|Event publication date=2025-01-10|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119288600|Publication stage code=A|Publication date=2025-01-10|Standardized publication number=CN119288600|Event publication date=2025-01-10|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-01-28|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-12-12|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN119288600|Publication stage code=B|Publication date=2025-12-12|Standardized publication number=CN119288600B|Event publication date=2025-12-12|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN119288600)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQg6/zI3DAuIRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080083091&ekey=2218&xpn=CN119288600B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=3WWlkuotmQaRgUXLDgSvxLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN119288600)|CN|(CN119288600)|CN (CN119288600)|NAME=TAIYUAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN|(CN119288600)|NAME=TAIYUAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN119288600)|NAME=SHEN YANLING;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY , REG=14101|(CN119288600)|NAME=SHEN YANLING;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY , REG=14101 (CN119288600)|CN| (CN119288600)|NAME=FENG GUORUI, COUNTRY=CN |NAME=WU GUOWEI|NAME=BAI JINWEN|NAME=HAN YANNA|NAME=MA JUNBIAO|NAME=LI XIRAN|NAME=SU SHENGYU|NAME=WU FAN|(CN119288600)|NAME=FENG GUORUI|NAME=WU GUOWEI|NAME=BAI JINWEN|NAME=HAN YANNA|NAME=MA JUNBIAO|NAME=LI XIRAN|NAME=SU SHENGYU|NAME=WU FAN 0 1 Titre: (CN119288600)|Carbon fixation filling method based on synchronous mining of coal-aluminum symbiotic ore deposit Résumé: (CN119288600)|The invention discloses a carbon sequestration filling method based on coal-aluminum symbiotic deposit synchronous mining, and belongs to the technical field of mining. The method comprises the following steps: S1, synchronously mining lower-layer aluminum ore and upper-layer coal mine; s2, coal gangue generated by coal mining is crushed to serve as filling aggregate; s3, performing carbon sequestration and dealkalization treatment on the red mud generated by aluminum ore smelting to be used as a filling cementing material; s4, mixing the two treated solid wastes, and matching cement to meet the relevant national standard of the filling material; and S5, pumping to a coal mine and aluminum mine goaf through a pipeline system to realize carbon sequestration filling. 7 Abstract gpt-4o-mini no The method focuses on carbon sequestration filling using mining byproducts and does not involve accelerated weathering of silicate or alkaline minerals for CO₂ capture.
5 CN202211267711 CN202211267711 CN115947333|CN115947333 104513816 CN115947333 B 2026-02-06 [CN115947333B]|CN115947333 A 2023-04-11 [CN115947333] 2022-10-17 2022-10-17 2026-02-06|2023-04-11 (CN115947333B)|2026-02-06 (CN115947333)|2042-10-17 (CN115947333)|Preparation method of dead-falling object-based biochar and soil carbon fixation method (CN115947333)|The invention discloses a preparation method of litter-based biochar and a soil carbon sequestration method. The preparation method of the litter-based biochar comprises the following steps: (1) collecting litters as a coarse material, and crushing the coarse material to obtain a fine material; (2) drying the fine material, and then pelletizing and molding; and (3) carrying out thermal cracking on the pressed particles to prepare the litter-based biochar. According to the method, waste biomass such as litters with small volume weight is firstly granulated and then pyrolyzed, so that the yield and the stability of the biochar are remarkably improved, and the carbon sequestration and emission reduction potential of the biochar in soil is remarkably improved. Through the technical means, the carbon sequestration rate of the litter-based biochar and the stability of the litter-based biochar are enhanced, and then the carbon sequestration and emission reduction potential of the litter-based biochar in soil is improved. Compared with non-pelletized biochar, the pelletized biochar produced by the invention has better yield, carbon content, carbon stability and soil carbon sequestration and emission reduction potential. ZHEJIANG UNIVERSITY HANGZHOU GLOBAL SCIENTIFIC & TECHNOLOGICAL INNOVATION CENTER (CN115947333)|ZHEJIANG UNIVERSITY HANGZHOU GLOBAL SCIENTIFIC AND TECHNOLOGICAL INNOVATION CENTER ([CN])|(CN115947333)|ZHEJIANG UNIVERSITY HANGZHOU GLOBAL SCIENTIFIC AND TECHNOLOGICAL INNOVATION CENTER ([CN]) WANG LIN|CHEN DINGJIANG|DUAN TONGZHOU|ZHU LIZHONG (CN115947333)|WANG LIN|CHEN DINGJIANG|DUAN TONGZHOU|ZHU LIZHONG|(CN115947333)|WANG LIN|CHEN DINGJIANG|DUAN TONGZHOU|ZHU LIZHONG (CN115947333)|SHEN JINLONG;HANGZHOU TIANQIN INTELLECTUAL PROPERTY AGENCY CO LTD|Reg. Nb: 33224 (CN115947333)|1. The soil carbon fixing method is characterized by comprising the following steps of: S1, preparing a dead object into dead object-based biochar; s2, applying the litter-based biochar to farmland soil; The preparation method of the dead object-based biochar in the step S1 comprises the following steps of: (1) Collecting the dead and falling matters as coarse materials, and crushing the coarse materials to obtain fine materials; (2) Drying the fine materials at the temperature of 120-160 ℃, controlling the moisture content of the dried fine materials to 15-20%, then pressing the fine materials into granules, forming the granules, using a granule pressing machine during granule pressing, controlling the pressure of the granules to 70-200 MPa during granule pressing, and controlling the density of the granules obtained after granule pressing to 1.1-1.4 kg/m 3; (3) And (3) thermally cracking the pressed particles to obtain the dead-drop-based biochar, wherein the thermal cracking temperature is 600-700 ℃. | (CN115947333)|The invention also provides a soil carbon fixing method, which comprises the following steps:|The invention discloses a preparation method of a dead-drop-based biochar and a soil carbon fixation method.|The invention provides a preparation method of sludge-based biochar and the sludge-based biochar, which comprise the following steps of S1, adding acid and water into sludge for stirring, injecting the mixture into a sludge chamber, S2, placing electrolyte into a cathode chamber, placing water into an anode chamber, adjusting the pH value of the cathode chamber to be acidic, wherein the cathode chamber, the sludge chamber and the anode chamber are sequentially separated by a porous partition board and filter paper, S3, respectively inserting electrodes into the cathode chamber and the anode chamber, switching on a power supply, stirring sludge in the sludge chamber, S4, centrifugally dehydrating, drying, grinding and sieving the sludge obtained in the step S3, S5, pyrolyzing the sludge obtained in the step S4 under the protection of inert gas, and cooling to obtain the sludge-based biochar.| (CN115947333)|SOIL CARBON FIXATION(100,6)|SLUDGE BIOCHAR(100,3)|DEAD FALLING OBJECT BIOCHAR(100,1)|GRANULE PRESSING(66,2)|DEAD DROP BIOCHAR(58,8)|CATHODE CHAMBER(58,4)|NONPRESSED GRANULAR BIOCHAR(58,2)|SLUDGE CHAMBER(57,3)|GRANULE(54,8)|ANODE CHAMBER(50,3)|GRANULE PRESSING MACHINE(48,1)|LITTER BIOCHAR(47,5)|POROUS PARTITION BOARD(45,1)|DEAD OBJECT BIOCHAR(38,2)|STIRRING SLUDGE(38,1)|FARMLAND SOIL(36,4)|PLACING ELECTROLYTE(34,1)|BRANCH LITTER(33,1)|LEAVE LITTER(33,1)|SLUDGE(32,4)|ELECTRODE INSERTION(30,1)|PRESSED PARTICLE(29,2)|GRANULE PRESSURE(29,1)|WASTE BIOMASS(28,2)|BIOCHAR STABILITY(27,2)|DEAD DROP BIOLOGICAL CARBON(26,4)|FALLING MATTER(24,2)|MOISTURE CONTENT(23,3)|COARSE MATERIAL(21,7)|COLLECTING DEAD DROP(21,1)|FINE MATERIAL(19,15)|CRACKING TEMPERATURE(19,4)|CRUSHING TREATMENT(19,2)|GRINDING(18,1)|DEAD MATTER(17,6)|ACID ADDITION(17,1)|SOIL CARBON(16,4)|FIXING CARBON(16,1)|GROUND(15,24)|DEAD(15,3)|OBJECT BIOCHAR(15,2)|DEAD OBJECT(14,1)|CARBON STABILITY(13,3)|DRIED FINE MATERIAL(13,1)|EMISSION REDUCTION POTENTIAL(11,2)|DEAD DROP SUBSTANCE BIOCHAR(10,3)|FRAGMENTED BIOCHAR(10,2)|FILTER PAPER(10,1)|SOIL EMISSION(8,3)|PADDY SOIL(8,2)|PYROLYSIS FURNACE(8,2)|INERT GAS(8,1)|BIOCHAR DECOMPOSITION(7,1)|PREPARING BIOCHAR DEFECT(7,1)|LETTER(6,6)|PELLETIZATION(6,4)|BIOCHAR CARBON CONTENT(6,2)|BIOCHAR CARBON DEFECT(6,1)|BIOMASS THERMAL CRACKING(6,1)|CARBONIZATION FURNACE(6,1)|FIRED BIOCHAR(6,1)|HARVESTED STRAW(6,1)|POULTRY MANURE(6,1)|CARBON NEUTRALIZATION(5,2)|RESTRICTIVE DIFFERENCE(5,2)|BIOCHAR CAPABILITY(5,1)|BIOCHAR INFLUENCE(5,1)|CRUCIBLE CUP(5,1)|FOREST FARM(5,1)|POWER SUPPLY(5,1)|PRESSED BIOCHAR(5,1)|PRESSED GRAIN BIOCHAR PERFORMANCE(5,1)|SIMULATION EXPERIMENT(5,1)|WITHERED BRANCH(5,1)|WITHERED LEAVE(5,1)|SMALL VOLUME WEIGHT(4,4)|CONFIDENCE(4,2)|FINE MATERIAL DIAMETER(4,2)|OXYGEN LIMITATION(4,2)|BIOCHAR QUALITY(4,1)|BIOCHAR YIELD COMPARISON(4,1)|BROKEN BIOCHAR(4,1)|CRACKING CARBON SEQUESTRATION(4,1)|GRANULATOR MODEL(4,1)|PELLETING MACHINE(4,1)|PULVERIZATION TREATMENT(4,1)|CARBON FIXATION RATE(3,3)|ASH(3,2)|AROMATICITY(3,1)|BIOCHAR CARBON ELEMENT DEFECT(3,1)|CARBON BALANCE(3,1)|ENHANCING YIELD(3,1)|JIANGZHE REGION(3,1)|OXYGEN INSULATION(3,1)|PRODUCING BIOCHAR(3,1)|RESOURCE VOLUME(3,1)|SOIL CARBON SEQUESTRATION(3,1)|SOIL COLUMN CARBON FIXATION(3,1)|SOIL DEPTH(3,1)|ACCUMULATED EMISSION VALUE(2,1)|AIRING(2,1)|AROMATIC CARBON CONTENT(2,1)|CARBON MEASUREMENT STABILITY(2,1)|COMPACTION(2,1)|CRUSHER(2,1)|DEFECT STATUS DATA(2,1)||(CN115947333)|LITTER BIOCHAR(100,23)|SOIL CARBON SEQUESTRATION(100,9)|FALLEN SUBSTANCE BIOCHAR(43,3)|LITTER BIOMASS CHARCOAL(39,4)|PREPARING BIOCHAR DEFECT(30,1)|SUBSTANCE BIOCHAR(29,3)|WITHERED BIOMASS(26,1)|NONGRANULATED BIOCHAR(22,2)|LITTER(19,16)|CRACK(15,6)|BIOCHAR STABILITY(14,2)|WASTE BIOMASS(14,2)|BIOCHAR(13,28)|LITTER BRANCH(13,2)|LITTER LEAVE(13,2)|GRANULE(13,1)|GRANULATION(12,6)|FARMLAND SOIL(12,4)|COARSE MATERIAL(11,6)|PELLETIZING(10,4)|PULVERIZATION TREATMENT(10,3)|PELLETIZATION(10,1)|CARBON SEQUESTRATION(9,11)|FINE MATERIAL(9,9)|MOISTURE CONTENT(8,3)|GROUND(7,21)|PELLETIZER(7,2)|STALK(7,1)|EMISSION REDUCTION(6,11)|FRAGMENTED BIOCHAR(6,3)|SLUDGE BIOCHAR(6,3)|BYIN(6,1)|FALLEN BIOMASS BIOCHAR(6,1)|FOREST FARM LITTER(6,1)|WITHERED MATTER(5,3)|DRYING TEMPERATURE(5,2)|EMISSION REDUCTION POTENTIAL(5,2)|DRY LAND SEQUESTRATION(4,2)|LITTER BIOLOGICAL CARBON(4,2)|PYROLYSIS FURNACE(4,2)|BIOCHAR DECOMPOSITION(4,1)|BIOCHAR INDUCTION(4,1)|FIRED BIOCHAR YIELD(4,1)|PRESSED GRANULAR BIOCHAR(4,1)|PYROLIGNEOUS LIQUOR(4,1)|LETTER(3,6)|ANODE CHAMBER(3,3)|FALLEN MATTER(3,3)|SLUDGE CHAMBER(3,3)|BIOCHAR CAPABILITY(3,1)|BIOCHAR CARBON DEFECT(3,1)|BIOMASS THERMAL CRACKING(3,1)|CENTRIFUGAL DEHYDRATION(3,1)|CRUCIBLE CUP(3,1)|GRANULATOR MODEL(3,1)|GRANULE COMPACTION(3,1)|HARVESTED STRAW(3,1)|PADDY SOIL(3,1)|PELLETED BIOCHAR(3,1)|POULTRY MANURE(3,1)|PREPARED LITTER BIOCHAR PARTICLE(3,1)|SIMULATION EXPERIMENT(3,1)|CRACKING TEMPERATURE(2,5)|FINE PARTICLE(2,5)|CARBON NEUTRALIZATION(2,2)|CONFIDENCE(2,2)|DIFFERENCE RESTRICTION(2,2)|INCLUSION(2,2)|OXYGEN LIMITATION(2,2)|PRESSED PARTICLE(2,2)|SMALL VOLUME WEIGHT(2,2)|AROMATICITY(2,1)|BIOCHAR CARBON ELEMENT DEFECT(2,1)|BIOCHAR DEFECT DATA(2,1)|BIOCHAR QUALITY(2,1)|CARBON BALANCE(2,1)|CARRYING OUT CARBON SEQUESTRATION(2,1)|CATHODE CHAMBER PH(2,1)|CRACKINGTHE RATE(2,1)|ELECTRODE INSERTION(2,1)|LOCKED CARBON(2,1)|MODIFIED LIQUOR(2,1)|OXYGEN INSULATION(2,1)|PELLETING(2,1)|PRODUCING BIOCHAR(2,1)|RELEASED FLUX(2,1)|SOIL CARBON DIOXIDE FLUX(2,1)|SOIL COLUMN CARBON SEQUESTRATION(2,1)|STIRRING SLUDGE(2,1)|TEMPERATURE BIOCHAR ORG(2,1)|AROMATIC CARBON CONTENT(1,1)|CARBON THERMAL(1,1)|CRUSHER(1,1)| (CN115947333)|1. The soil carbon fixing method is characterized by comprising the following steps of:| S1, preparing a dead object into dead object-based biochar; | s2, applying the litter-based biochar to farmland soil; | The preparation method of the dead object-based biochar in the step S1 comprises the following steps of: | (1) Collecting the dead and falling matters as coarse materials, and crushing the coarse materials to obtain fine materials; | (2) Drying the fine materials at the temperature of 120-160 ℃, controlling the moisture content of the dried fine materials to 15-20%, then pressing the fine materials into granules, forming the granules, using a granule pressing machine during granule pressing, controlling the pressure of the granules to 70-200 MPa during granule pressing, and controlling the density of the granules obtained after granule pressing to 1.1-1.4 kg/m 3; | (3) And (3) thermally cracking the pressed particles to obtain the dead-drop-based biochar, wherein the thermal cracking temperature is 600-700 ℃. |2. The method of claim 1, wherein the litter is at least one of a litter of leaves, a litter of branches, and a straw.|3. The method for fixing carbon in soil according to claim 1, wherein in the step (1), the diameter of the fine material obtained after the crushing treatment is 1-2 mm and the length thereof is 1-20 mm. (CN115947333)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of carbon neutralization, and particularly relates to a preparation method of a dead-drop substance-based biochar and a soil carbon fixing method.|BACKGROUND ART|[0002] Plants fix carbon dioxide in the atmosphere through photosynthesis, and the fixed carbon is released back to the atmosphere through respiration and decomposition to form macroscopic carbon cycle, which maintains the overall carbon balance. A large number of litter are produced annually worldwide, most of the carbon in the litter entering the atmosphere after a short period of decay in the form of carbon dioxide. If the carbon in the dead matters is locked in the form of biochar and then added into soil for carbon sequestration, the carbon in the dead matters can be prevented from being quickly decomposed and returned to the atmosphere, so that the concentration of carbon dioxide in the atmosphere is reduced, and the effects of carbon sequestration and emission reduction are achieved.|[0003] The dead matters have smaller volume weight, most ash is formed after direct pyrolysis, and most of contained carbon elements return to the atmosphere in the form of carbon dioxide, so that the fired biochar has lower yield and poor aromaticity and stability. Therefore, the method has important significance for improving the carbon fixation and emission reduction potential of the dead-drop substance-based biochar in soil, and mainly comprises the potential for improving the carbon unlocking capability of the biochar and reducing the emission of greenhouse gases such as carbon dioxide in soil.|[0004] Carbon content, aromatic carbon content, H/C org, defects and the like of the biochar are important indexes for measuring carbon stability, and the carbon stability can influence the decomposition of the biochar in a soil system and the induced organic carbon excitation effect of the soil, so that the apparent carbon-nitrogen related greenhouse gas emission flux of the soil is disturbed, and further the carbon sequestration potential of the dead-drop substance-based biochar in the soil is influenced. The biomass raw materials commonly used for producing the biochar at present mainly comprise crop straws, forest waste, poultry manure, sludge, algae and the like.|[0005] For example, the invention with publication number CN109775684A discloses a method for preparing biochar by using rice straw, which comprises the following steps of selecting the harvested straw and carrying out piling and airing. The invention adopts the straw with extremely low cost as the raw material of the biochar, and pulverizes and dries the straw in advance, then burns the straw through the carbonization furnace, and matches the conveying device and the cooling device with the straw, so that the straw is burned and cooled, the production line operation can be formed, then wood vinegar liquid generated by burning the straw is diluted with pure water according to a proportion, the modified liquid is formed, the modification cost of the biochar is greatly reduced, and finally the biochar is sieved, so that the biochar reaches the specification particle size.|[0006] The invention provides a preparation method of sludge-based biochar and the sludge-based biochar, which comprise the following steps of S1, adding acid and water into sludge for stirring, injecting the mixture into a sludge chamber, S2, placing electrolyte into a cathode chamber, placing water into an anode chamber, adjusting the pH value of the cathode chamber to be acidic, wherein the cathode chamber, the sludge chamber and the anode chamber are sequentially separated by a porous partition board and filter paper, S3, respectively inserting electrodes into the cathode chamber and the anode chamber, switching on a power supply, stirring sludge in the sludge chamber, S4, centrifugally dehydrating, drying, grinding and sieving the sludge obtained in the step S3, S5, pyrolyzing the sludge obtained in the step S4 under the protection of inert gas, and cooling to obtain the sludge-based biochar.|[0007] The dead matters are rich in resources, but have smaller volume weight, and the ash is basically burned in the natural environment without limiting oxygen, so the utilization rate is very low. If the technical means can be used for enhancing the yield of biochar produced by the dead drop and the stability of the dead drop-based biochar, the dead drop with a plurality of resource volumes can be used for carrying out soil carbon fixation and emission reduction, so that an important technical means is provided for carbon neutralization, and the atmospheric temperature chamber effect is relieved.|DISCLOSURE|Disclosure of Invention|[0008] Aiming at the defects of preparing biochar by using a dead drop and carrying out carbon fixation and emission reduction utilization in the prior art, the invention provides a preparation method of dead drop-based biochar and a soil carbon fixation method.|[0009] A preparation method of a litter-based biochar comprises the following steps:|[0010] (1) Collecting the dead and falling matters as coarse materials, and crushing the coarse materials to obtain fine materials; |[0011] (2) Drying the fine materials, and then pressing and forming; |[0012] (3) And (3) thermally cracking the pressed particles to obtain the dead-drop-based biochar. |[0013] The withered object is at least one of withered leaves, withered branches and straws.|[0014] Preferably, in the step (1), the diameter of the fine material obtained after the crushing treatment is 1-2 mm, and the length of the fine material is 1-20 mm. If the particle size of the fine powder obtained at the time of the pulverization treatment is too large, the effect of granulation may be poor.|[0015] Preferably, in the step (2), the drying temperature is 120-160 ℃, and the moisture content after drying is controlled to be 15-20%.|[0016] Preferably, in the step (2), a pelleting machine is used during pelleting, and the pressure is controlled to be 70-200 mpa during pelleting.|[0017] Preferably, in the step (2), the density of the granules obtained after pelleting is 1.1-1.4 kg/m 3. The density of the granules is about 0.10-0.25 kg/m 3 before pressing.|[0018] Preferably, in the step (3), the thermal cracking temperature is 300-700 ℃. In an alternative, the thermal cracking temperature is 300-500 ℃. In an alternative mode, the thermal cracking temperature is 600-700 ℃. Oxygen limitation is needed in the thermal cracking process, but no oxygen insulation is needed, so that nitrogen is not needed to be introduced, and the cost can be saved.|[0019] The yield of the biochar refers to the quality of the biochar produced by biomass preparation per unit mass, and the carbon fixation potential of the biochar for improving soil comprises the following two aspects of locking carbon quantity (m Carbon locking amount =m Amount of biomass used times the yield of the biochar and the carbon content of the biochar) of the biochar per se and the influence of the biochar on the flux of carbon dioxide, methane or nitrous oxide (converted into carbon dioxide equivalent) of the soil within a certain time limit.|[0020] The invention also provides a soil carbon fixing method, which comprises the following steps:|[0021] (1) Preparing the litter into litter-based biochar by using the litter-based biochar preparation method; |[0022] (2) The litter-based biochar is applied to farmland soil. |[0023] The prepared dead object-based biochar particles are applied to farmland soil, so that on one hand, the soil property is optimized as a soil conditioner, and on the other hand, carbon sequestration is carried out, and the effects of carbon fixation and emission reduction are exerted. The method is applied to farmland soil, and is characterized in that the dead and falling object-based biochar is uniformly mixed into surface soil, and the soil depth is 10-20 cm.|[0024] According to the invention, the waste biomass such as dead matters with smaller volume weight is firstly pressed into granules and then pyrolyzed, so that the yield and stability of the biochar and the carbon fixation and emission reduction potential of the biochar in soil are obviously increased. Through the technical means, the carbon fixation rate of the biological carbon produced by the dead drop and the stability of the dead drop-based biological carbon are enhanced, and the carbon fixation and emission reduction potential of the dead drop-based biological carbon in soil is further improved. Compared with the non-pressed granular biochar, the pressed granular biochar produced by the method has better yield, carbon content, carbon stability and soil carbon fixation and emission reduction potential.|DRAWINGS DESCRIPTION|[0025] FIG. 1 is a graph showing the comparison results of different biochar yields (a), different biochar carbon contents (b) and different biochar carbon fixation rates (c).|[0026] FIG. 2 is a graph showing comparison results of different biochar H/C org (a) and different biochar carbon element defects (b).|[0027] FIG. 3 is a graph showing the comparison of the time sequence relationships (a-e) of the emission flux of the soil CO 2 induced by different biochars and the accumulated emission value (f) of the soil CO 2 induced by different biochars.|INVENTION MODE|Detailed Description|[0028] Example 1|[0029] Collecting the dry falling objects in a forest farm in Zunyi state, crushing the dry falling objects coarse materials into fine materials with the diameter range of 1-2 mm and the length range of 1-20 mm by using a crusher, marking the fine materials as an 'unpressed biomass raw material A', drying the fine materials at the temperature of 120-160 ℃ (the moisture content is controlled to be 15% -20%), performing compression molding by using a granulator, marking the fine materials as a 'pressed biomass raw material B' (the granulator model is XGJ560, the pressure is controlled to be about 120 Mpa), and the particle density is 1.1-1.4 kg/m 3 after pressing. 10 different kinds of biochar are prepared from raw materials A and B at 300 ℃,400 ℃, 500 ℃, 600 ℃ and 700 ℃ respectively, and the biochar is respectively named BC300-A, BC400-A, BC500-A, BC500-A, BC-A, BC-B, BC400-B, BC500-B, B600C-B, BC-700-B.|[0030] The method comprises the steps of (1) filling biomass raw materials into a crucible cup, feeding the crucible cup into a pyrolysis furnace for thermal cracking, 2, heating the pyrolysis furnace to 80 ℃ for preheating, then heating to a target temperature at a heating rate of 5 ℃ per minute, 3, stopping heating after pyrolysis at the target temperature for 2 hours, taking out the produced biochar after cooling, and no nitrogen is required to be introduced in the whole process.|[0031] The productivity, carbon content, carbon locking rate (carbon fixation rate), H/C org and defects of each biochar were measured separately.|[0032] TABLE 1 comparison of different biochar yields, carbon fixation rates and defect status data|[0033] |[0034] Note that 1, the values in brackets represent the standard deviation of the samples (confidence 95% ci), 2, the letters a, b, c, etc. after brackets represent the restrictive differences, the same letters indicate no significant differences between groups, the different letters indicate significant differences between groups, and P <0.05.|[0035] The experimental results are shown in fig. 1, 2 and table 1. Fig. 1 fully demonstrates that for biochar fired at any temperature from low (300 ℃) to high (700 ℃) the pelletization can significantly increase the yield of biochar, thereby greatly increasing the number of biochar bases available for soil carbon sequestration per year, that pelletization can significantly increase the carbon content of biochar produced at medium and high temperatures (600 ℃ and 700 ℃), that pelletization can significantly increase the production carbon sequestration rate or thermal cracking carbon sequestration rate (yield multiplied by carbon content) of biochar produced at each temperature, and that this effect is most pronounced at medium and high temperatures (600 ℃ and 700 ℃). Fig. 2a shows that pelletization increases H/C org of the low temperature biochar (300-500 ℃) without significant impact on H/C org of the medium and high temperature biochar. Figure 2b shows that the compaction reduces the carbon defects of the biochar at various temperatures (most significant reduction of carbon defects for high temperature biochar), thereby enhancing the stability and oxidation resistance of the carbon in the biochar and ultimately enhancing its carbon fixation potential in the soil.|[0036] Example 2|[0037] 10 Kinds of biochar (comprising BC300-A, BC400-A, BC500-A, BC600-A, BC700-A, BC300-B, BC400-B, BC500-B, B600C-B, BC 700-B) fired in example 1 are respectively added into typical paddy soil in a Jiangzhe region to serve as an experimental group, a soil column only containing paddy soil without the biochar is taken as a control group, a soil column carbon fixation simulation experiment is carried out, the soil surface CO 2 discharge flux of different soil columns is measured, and the performance of the pressed grain biochar for better reducing the soil CO 2 discharge compared with the broken biochar is examined and verified.|[0038] Short-term impact of high temperature biochar on soil CO 2 release flux in Table 2|[0039] |[0040] Note that 1, the values in brackets represent the standard deviation of the samples (confidence 95% ci), 2, the letters a, b, c, etc. after brackets represent the restrictive differences, the same letters indicate no significant differences between groups, the different letters indicate significant differences between groups, and P <0.05.|[0041] The experimental results are shown in FIG. 3 and Table 2. As can be seen from fig. 3a, 3b, 3C, for low temperature biochar (300-500 ℃), there is no significant difference in the discharge flux of the pressed and fragmented biochar for soil CO 2. As can be seen from fig. 3d, 3e, for medium and high temperature biochar (600 ℃ and 700 ℃) the pressed granular biochar has better, more significant performance in reducing the emission of soil CO 2 than the fragmented biochar. The comparison of the accumulated CO 2 emission values of the soil induced by different biochars in FIG. 3f can further prove that the pelleting can effectively reduce the CO 2 emission of the soil in the presence of the medium-high temperature biochar, thereby enhancing the carbon fixation and emission reduction potential of the biochar in the soil.|[0042] By combining the results of examples 1 and 2, it can be fully demonstrated that the pelletization can significantly increase the yield in the oxygen-limited thermal cracking process of biochar at each temperature, the production carbon fixation rate or thermal cracking carbon fixation rate (yield multiplied by carbon fixation rate) of biochar produced at each temperature, thereby greatly increasing the number of biochar usable for soil carbon fixation per year. Meanwhile, the carbon content of the medium-high temperature biochar (600 ℃ and 700 ℃) can be obviously increased by pelleting, the defect of carbon is reduced, and the emission of soil CO 2 in a short period is reduced. In conclusion, the biochar produced by pelleting before biomass thermal cracking can effectively improve the carbon fixation rate of the dead-drop-based biochar and the carbon fixation and emission reduction potential of soil. (CN115947333)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of carbon neutralization, and particularly relates to a preparation method of a dead-drop substance-based biochar and a soil carbon fixing method.|BACKGROUND ART|[0002] Plants fix carbon dioxide in the atmosphere through photosynthesis, and the fixed carbon is released back to the atmosphere through respiration and decomposition to form macroscopic carbon cycle, which maintains the overall carbon balance. A large number of litter are produced annually worldwide, most of the carbon in the litter entering the atmosphere after a short period of decay in the form of carbon dioxide. If the carbon in the dead matters is locked in the form of biochar and then added into soil for carbon sequestration, the carbon in the dead matters can be prevented from being quickly decomposed and returned to the atmosphere, so that the concentration of carbon dioxide in the atmosphere is reduced, and the effects of carbon sequestration and emission reduction are achieved.|[0003] The dead matters have smaller volume weight, most ash is formed after direct pyrolysis, and most of contained carbon elements return to the atmosphere in the form of carbon dioxide, so that the fired biochar has lower yield and poor aromaticity and stability. Therefore, the method has important significance for improving the carbon fixation and emission reduction potential of the dead-drop substance-based biochar in soil, and mainly comprises the potential for improving the carbon unlocking capability of the biochar and reducing the emission of greenhouse gases such as carbon dioxide in soil.|[0004] Carbon content, aromatic carbon content, H/C org, defects and the like of the biochar are important indexes for measuring carbon stability, and the carbon stability can influence the decomposition of the biochar in a soil system and the induced organic carbon excitation effect of the soil, so that the apparent carbon-nitrogen related greenhouse gas emission flux of the soil is disturbed, and further the carbon sequestration potential of the dead-drop substance-based biochar in the soil is influenced. The biomass raw materials commonly used for producing the biochar at present mainly comprise crop straws, forest waste, poultry manure, sludge, algae and the like.|[0005] For example, the invention with publication number CN109775684A discloses a method for preparing biochar by using rice straw, which comprises the following steps of selecting the harvested straw and carrying out piling and airing. The invention adopts the straw with extremely low cost as the raw material of the biochar, and pulverizes and dries the straw in advance, then burns the straw through the carbonization furnace, and matches the conveying device and the cooling device with the straw, so that the straw is burned and cooled, the production line operation can be formed, then wood vinegar liquid generated by burning the straw is diluted with pure water according to a proportion, the modified liquid is formed, the modification cost of the biochar is greatly reduced, and finally the biochar is sieved, so that the biochar reaches the specification particle size.|[0006] The invention provides a preparation method of sludge-based biochar and the sludge-based biochar, which comprise the following steps of S1, adding acid and water into sludge for stirring, injecting the mixture into a sludge chamber, S2, placing electrolyte into a cathode chamber, placing water into an anode chamber, adjusting the pH value of the cathode chamber to be acidic, wherein the cathode chamber, the sludge chamber and the anode chamber are sequentially separated by a porous partition board and filter paper, S3, respectively inserting electrodes into the cathode chamber and the anode chamber, switching on a power supply, stirring sludge in the sludge chamber, S4, centrifugally dehydrating, drying, grinding and sieving the sludge obtained in the step S3, S5, pyrolyzing the sludge obtained in the step S4 under the protection of inert gas, and cooling to obtain the sludge-based biochar.|[0007] The dead matters are rich in resources, but have smaller volume weight, and the ash is basically burned in the natural environment without limiting oxygen, so the utilization rate is very low. If the technical means can be used for enhancing the yield of biochar produced by the dead drop and the stability of the dead drop-based biochar, the dead drop with a plurality of resource volumes can be used for carrying out soil carbon fixation and emission reduction, so that an important technical means is provided for carbon neutralization, and the atmospheric temperature chamber effect is relieved.|DISCLOSURE|Disclosure of Invention|[0008] Aiming at the defects of preparing biochar by using a dead drop and carrying out carbon fixation and emission reduction utilization in the prior art, the invention provides a preparation method of dead drop-based biochar and a soil carbon fixation method.|[0009] A preparation method of a litter-based biochar comprises the following steps:|[0010] (1) Collecting the dead and falling matters as coarse materials, and crushing the coarse materials to obtain fine materials; |[0011] (2) Drying the fine materials, and then pressing and forming; |[0012] (3) And (3) thermally cracking the pressed particles to obtain the dead-drop-based biochar. |[0013] The withered object is at least one of withered leaves, withered branches and straws.|[0014] Preferably, in the step (1), the diameter of the fine material obtained after the crushing treatment is 1-2 mm, and the length of the fine material is 1-20 mm. If the particle size of the fine powder obtained at the time of the pulverization treatment is too large, the effect of granulation may be poor.|[0015] Preferably, in the step (2), the drying temperature is 120-160 ℃, and the moisture content after drying is controlled to be 15-20%.|[0016] Preferably, in the step (2), a pelleting machine is used during pelleting, and the pressure is controlled to be 70-200 mpa during pelleting.|[0017] Preferably, in the step (2), the density of the granules obtained after pelleting is 1.1-1.4 kg/m 3. The density of the granules is about 0.10-0.25 kg/m 3 before pressing.|[0018] Preferably, in the step (3), the thermal cracking temperature is 300-700 ℃. In an alternative, the thermal cracking temperature is 300-500 ℃. In an alternative mode, the thermal cracking temperature is 600-700 ℃. Oxygen limitation is needed in the thermal cracking process, but no oxygen insulation is needed, so that nitrogen is not needed to be introduced, and the cost can be saved.|[0019] The yield of the biochar refers to the quality of the biochar produced by biomass preparation per unit mass, and the carbon fixation potential of the biochar for improving soil comprises the following two aspects of locking carbon quantity (m Carbon locking amount =m Amount of biomass used times the yield of the biochar and the carbon content of the biochar) of the biochar per se and the influence of the biochar on the flux of carbon dioxide, methane or nitrous oxide (converted into carbon dioxide equivalent) of the soil within a certain time limit.|[0020] The invention also provides a soil carbon fixing method, which comprises the following steps:|[0021] (1) Preparing the litter into litter-based biochar by using the litter-based biochar preparation method; |[0022] (2) The litter-based biochar is applied to farmland soil. |[0023] The prepared dead object-based biochar particles are applied to farmland soil, so that on one hand, the soil property is optimized as a soil conditioner, and on the other hand, carbon sequestration is carried out, and the effects of carbon fixation and emission reduction are exerted. The method is applied to farmland soil, and is characterized in that the dead and falling object-based biochar is uniformly mixed into surface soil, and the soil depth is 10-20 cm.|[0024] According to the invention, the waste biomass such as dead matters with smaller volume weight is firstly pressed into granules and then pyrolyzed, so that the yield and stability of the biochar and the carbon fixation and emission reduction potential of the biochar in soil are obviously increased. Through the technical means, the carbon fixation rate of the biological carbon produced by the dead drop and the stability of the dead drop-based biological carbon are enhanced, and the carbon fixation and emission reduction potential of the dead drop-based biological carbon in soil is further improved. Compared with the non-pressed granular biochar, the pressed granular biochar produced by the method has better yield, carbon content, carbon stability and soil carbon fixation and emission reduction potential.|DRAWINGS DESCRIPTION|[0025] FIG. 1 is a graph showing the comparison results of different biochar yields (a), different biochar carbon contents (b) and different biochar carbon fixation rates (c).|[0026] FIG. 2 is a graph showing comparison results of different biochar H/C org (a) and different biochar carbon element defects (b).|[0027] FIG. 3 is a graph showing the comparison of the time sequence relationships (a-e) of the emission flux of the soil CO 2 induced by different biochars and the accumulated emission value (f) of the soil CO 2 induced by different biochars.|INVENTION MODE|Detailed Description|[0028] Example 1|[0029] Collecting the dry falling objects in a forest farm in Zunyi state, crushing the dry falling objects coarse materials into fine materials with the diameter range of 1-2 mm and the length range of 1-20 mm by using a crusher, marking the fine materials as an 'unpressed biomass raw material A', drying the fine materials at the temperature of 120-160 ℃ (the moisture content is controlled to be 15% -20%), performing compression molding by using a granulator, marking the fine materials as a 'pressed biomass raw material B' (the granulator model is XGJ560, the pressure is controlled to be about 120 Mpa), and the particle density is 1.1-1.4 kg/m 3 after pressing. 10 different kinds of biochar are prepared from raw materials A and B at 300 ℃,400 ℃, 500 ℃, 600 ℃ and 700 ℃ respectively, and the biochar is respectively named BC300-A, BC400-A, BC500-A, BC500-A, BC-A, BC-B, BC400-B, BC500-B, B600C-B, BC-700-B.|[0030] The method comprises the steps of (1) filling biomass raw materials into a crucible cup, feeding the crucible cup into a pyrolysis furnace for thermal cracking, 2, heating the pyrolysis furnace to 80 ℃ for preheating, then heating to a target temperature at a heating rate of 5 ℃ per minute, 3, stopping heating after pyrolysis at the target temperature for 2 hours, taking out the produced biochar after cooling, and no nitrogen is required to be introduced in the whole process.|[0031] The productivity, carbon content, carbon locking rate (carbon fixation rate), H/C org and defects of each biochar were measured separately.|[0032] TABLE 1 comparison of different biochar yields, carbon fixation rates and defect status data|[0033] |[0034] Note that 1, the values in brackets represent the standard deviation of the samples (confidence 95% ci), 2, the letters a, b, c, etc. after brackets represent the restrictive differences, the same letters indicate no significant differences between groups, the different letters indicate significant differences between groups, and P <0.05.|[0035] The experimental results are shown in fig. 1, 2 and table 1. Fig. 1 fully demonstrates that for biochar fired at any temperature from low (300 ℃) to high (700 ℃) the pelletization can significantly increase the yield of biochar, thereby greatly increasing the number of biochar bases available for soil carbon sequestration per year, that pelletization can significantly increase the carbon content of biochar produced at medium and high temperatures (600 ℃ and 700 ℃), that pelletization can significantly increase the production carbon sequestration rate or thermal cracking carbon sequestration rate (yield multiplied by carbon content) of biochar produced at each temperature, and that this effect is most pronounced at medium and high temperatures (600 ℃ and 700 ℃). Fig. 2a shows that pelletization increases H/C org of the low temperature biochar (300-500 ℃) without significant impact on H/C org of the medium and high temperature biochar. Figure 2b shows that the compaction reduces the carbon defects of the biochar at various temperatures (most significant reduction of carbon defects for high temperature biochar), thereby enhancing the stability and oxidation resistance of the carbon in the biochar and ultimately enhancing its carbon fixation potential in the soil.|[0036] Example 2|[0037] 10 Kinds of biochar (comprising BC300-A, BC400-A, BC500-A, BC600-A, BC700-A, BC300-B, BC400-B, BC500-B, B600C-B, BC 700-B) fired in example 1 are respectively added into typical paddy soil in a Jiangzhe region to serve as an experimental group, a soil column only containing paddy soil without the biochar is taken as a control group, a soil column carbon fixation simulation experiment is carried out, the soil surface CO 2 discharge flux of different soil columns is measured, and the performance of the pressed grain biochar for better reducing the soil CO 2 discharge compared with the broken biochar is examined and verified.|[0038] Short-term impact of high temperature biochar on soil CO 2 release flux in Table 2|[0039] |[0040] Note that 1, the values in brackets represent the standard deviation of the samples (confidence 95% ci), 2, the letters a, b, c, etc. after brackets represent the restrictive differences, the same letters indicate no significant differences between groups, the different letters indicate significant differences between groups, and P <0.05.|[0041] The experimental results are shown in FIG. 3 and Table 2. As can be seen from fig. 3a, 3b, 3C, for low temperature biochar (300-500 ℃), there is no significant difference in the discharge flux of the pressed and fragmented biochar for soil CO 2. As can be seen from fig. 3d, 3e, for medium and high temperature biochar (600 ℃ and 700 ℃) the pressed granular biochar has better, more significant performance in reducing the emission of soil CO 2 than the fragmented biochar. The comparison of the accumulated CO 2 emission values of the soil induced by different biochars in FIG. 3f can further prove that the pelleting can effectively reduce the CO 2 emission of the soil in the presence of the medium-high temperature biochar, thereby enhancing the carbon fixation and emission reduction potential of the biochar in the soil.|[0042] By combining the results of examples 1 and 2, it can be fully demonstrated that the pelletization can significantly increase the yield in the oxygen-limited thermal cracking process of biochar at each temperature, the production carbon fixation rate or thermal cracking carbon fixation rate (yield multiplied by carbon fixation rate) of biochar produced at each temperature, thereby greatly increasing the number of biochar usable for soil carbon fixation per year. Meanwhile, the carbon content of the medium-high temperature biochar (600 ℃ and 700 ℃) can be obviously increased by pelleting, the defect of carbon is reduced, and the emission of soil CO 2 in a short period is reduced. In conclusion, the biochar produced by pelleting before biomass thermal cracking can effectively improve the carbon fixation rate of the dead-drop-based biochar and the carbon fixation and emission reduction potential of soil. Family Number|(104513816)|104513816|Abstract|(CN115947333B B)|The invention discloses a preparation method of litter - based biochar and a soil carbon sequestration method . The preparation method of the litter - based biochar comprises the following steps : ( 1 ) collecting litters as a coarse material , and crushing the coarse material to obtain a fine material ; ( 2 ) drying the fine material , and then pelletizing and molding ; and ( 3 ) carrying out thermal cracking on the pressed particles to prepare the litter - based biochar . According to the method , waste biomass such as litters with small volume weight is firstly granulated and then pyrolyzed , so that the yield and the stability of the biochar are remarkably improved , and the carbon sequestration and emission reduction potential of the biochar in soil is remarkably improved . Through the technical means , the carbon sequestration rate of the litter - based biochar and the stability of the litter - based biochar are enhanced , and then the carbon sequestration and emission reduction potential of the litter - based biochar in soil is improved . Compared with non - pelletized biochar , the pelletized biochar produced by the invention has better yield , carbon content , carbon stability and soil carbon sequestration and emission reduction potential . |IPC codes|(CN115947333B B)|A01B - 079/02 |C01B - 032/05 |Title|(CN115947333 A)|Preparation method of litter - based biochar and soil carbon sequestration method | Basic materials chemistry|Materials, metallurgy|Other special machines A01B-079/00|A01B-079/02|A01C-021/00|C01B-032/05|C05D-007/00|C05D-009/00|C05F-003/00|C05F-011/08|C05G-003/80|C09K-017/00|C09K-017/02|C09K-017/04|C09K-017/40|C09K-2101/00|C09K-2109/00|Y02E-050/10 A01B-079/00|A01B-079/02|A01C-021/00|C01B-032/05|C05D-007/00|C05D-009/00|C05F-003/00|C05F-011/08|C05G-003/80|C09K-017/00|C09K-017/02|C09K-017/04|C09K-017/40|C09K-2101/00|C09K-2109/00|Y02E-050/10 A01B-079/02|C01B-032/05|C09K-017/02|C09K-101/00 A01B-079/02|C01B-032/05|C09K-017/02|C09K-101/00 CN116548107B CN116548107B 106037022 WHO=Examiner SELF=N CN112093789|CN110326385|CN107500265|CN112934951|CN105692586 CN112093789 91952297 WHO=Examiner SELF=N CAT=A|CN110326385 86298743 WHO=Examiner SELF=N CAT=A|CN107500265 78178393 WHO=Examiner SELF=N CAT=A|CN112934951 94681684 WHO=Examiner SELF=N|CN105692586 73373587 WHO=Examiner SELF=N CN107500265; CN110326385; CN112093789; CN105692586; CN112934951 GRANTED (CN115947333)|GRANTED ALIVE (CN115947333)|ALIVE (CN115947333)|LEGAL DETAILS FOR CN115947333|Actual or expected expiration date=2042-10-17|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-10-17|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211267711|Application date=2022-10-17|Standardized application number=2022CN-1267711|Event publication date=2023-04-11|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115947333|Publication stage code=A|Publication date=2023-04-11|Standardized publication number=CN115947333|Event publication date=2023-04-11|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-04-28|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2026-02-06|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN115947333|Publication stage code=B|Publication date=2026-02-06|Standardized publication number=CN115947333B|Event publication date=2026-02-06|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN115947333)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoROJznMkk5uAhj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080765491&ekey=2123&xpn=CN115947333B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=6LIaI1MmrZ%252BzeTJMGzTyLrmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN115947333)|CN|(CN115947333)|CN (CN115947333)|NAME=ZHEJIANG UNIVERSITY HANGZHOU GLOBAL SCIENTIFIC AND TECHNOLOGICAL INNOVATION CENTER , COUNTRY=CN|(CN115947333)|NAME=ZHEJIANG UNIVERSITY HANGZHOU GLOBAL SCIENTIFIC AND TECHNOLOGICAL INNOVATION CENTER , COUNTRY=CN (CN115947333)|NAME=SHEN JINLONG;HANGZHOU TIANQIN INTELLECTUAL PROPERTY AGENCY CO LTD , REG=33224|(CN115947333)|NAME=SHEN JINLONG;HANGZHOU TIANQIN INTELLECTUAL PROPERTY AGENCY CO LTD , REG=33224 (CN115947333)|CN| (CN115947333)|NAME=WANG LIN, COUNTRY=CN |NAME=CHEN DINGJIANG|NAME=DUAN TONGZHOU|NAME=ZHU LIZHONG|(CN115947333)|NAME=WANG LIN|NAME=CHEN DINGJIANG|NAME=DUAN TONGZHOU|NAME=ZHU LIZHONG 0 1 Titre: (CN115947333)|Preparation method of dead-falling object-based biochar and soil carbon fixation method Résumé: (CN115947333)|The invention discloses a preparation method of litter-based biochar and a soil carbon sequestration method. The preparation method of the litter-based biochar comprises the following steps: (1) collecting litters as a coarse material, and crushing the coarse material to obtain a fine material; (2) drying the fine material, and then pelletizing and molding; and (3) carrying out thermal cracking on the pressed particles to prepare the litter-based biochar. According to the method, waste biomass such as litters with small volume weight is firstly granulated and then pyrolyzed, so that the yield and the stability of the biochar are remarkably improved, and the carbon sequestration and emission reduction potential of the biochar in soil is remarkably improved. Through the technical means, the carbon sequestration rate of the litter-based biochar and the stability of the litter-based biochar are enhanced, and then the carbon sequestration and emission reduction potential of the litter-based biochar in soil is improved. Compared with non-pelletized biochar, the pelletized biochar produced by the invention has better yield, carbon content, carbon stability and soil carbon sequestration and emission reduction potential. 3 Abstract gpt-4o-mini no The article focuses on biochar production from litter and its carbon sequestration potential in soil, without addressing accelerated weathering or mineral carbonation processes related to CO₂ capture.
6 US15/932,758|US16/704,880 US16/704,880|US15/932,758 US11426695|US20200114310|US20190321777 86377114 US11426695 B2 2022-08-30 [US11426695]|US20200114310 A1 2020-04-16 [US20200114310]|US20190321777 A1 2019-10-24 [US20190321777] 2018-04-23|2019-12-05 2019-12-05|2018-04-23 2022-08-30|2020-04-16|2019-10-24 (US11426695)|2022-08-30| (US11426695)|2038-04-23|(US20190321777)|2020-01-05 (US11426695)|Media and air filters for carbon dioxide sequestration (US11426695)|Filter media and filters for the sequestration of carbon dioxide are disclosed. The carbon dioxide sequestering filter media incorporate silicate minerals, and the carbon dioxide sequestering filters incorporate carbon dioxide sequestering filter media. Filters using only carbon dioxide sequestering media and filters combining carbon dioxide sequestering media with traditional air filter media are disclosed. The carbon dioxide sequestering filters may be used instead of traditional air filters in residential, commercial and industrial applications. GERLACH RICHARD ([CA])|GERLACH RICHARD ([CA]) (US11426695)|Gerlach Richard ([CA])|(US20200114310)|GERLACH Richard ([CA])|(US20190321777)|Gerlach Richard ([CA]) GERLACH RICHARD (US11426695)|Gerlach Richard|(US20200114310)|GERLACH Richard (US11426695)|Kramer & Amado, P.C. (US11426695)|These media are particularly useful for deployment in ductworks in residential, commercial and industrial buildings.|Carbon dioxide, along with other greenhouse gases, are responsible for the greenhouse effect, which is causing the Earth's temperature to rise.|For all embodiments of a carbon dioxide sequestering air filter, since there is the possibility of damage to the filter allowing dust to be created from the silicate minerals, it is desirable from a safety point of view for the filter to be constructed so the air flows through a traditional air filter media as a last step before leaving the filter, and for the traditional air filter in this last step to be sized so as to control any escape of silicate mineral dust or particles.|The proposal to spread olivine or other silicate minerals on the earth would be energy intensive expensive, and time consuming.| (US11426695)|1. An air filter media comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media comprises a woven substrate and uncoated fibers of a silicate mineral, wherein the uncoated fibers are woven into the substrate; wherein the silicate mineral is at least one mineral selected from the group consisting of olivine, fayalite, fosterite, and serpentine; and wherein the carbon dioxide sequestering media is air-porous.|6. An air filter media comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media comprises a woven substrate and a plurality of yarns, wherein each yarn comprises at least two uncoated fibers of a silicate mineral twisted together; wherein the plurality of yarns are woven into the substrate; wherein the silicate mineral is at least one mineral selected from the group consisting of olivine, fayalite, fosterite, and serpentine; and wherein the carbon dioxide sequestering media is air-porous.|7. An air filter media comprising: an air-porous first substrate, an air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates an uncoated silicate mineral, wherein the silicate mineral is at least one mineral selected from the group consisting of olivine, fayalite, fosterite, and serpentine; and a bonding agent; wherein the bonding agent bonds the uncoated silicate minerals to the air-porous first substrate.| (US11426695)|In accordance with the invention, there is provided a carbon dioxide sequestering air filter media comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In a further aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers. In a further aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate and silicate mineral fibers. In another aspect of this invention, the particle size of the silicate minerals is between 1.0 mm and 0.01 mm. In a further aspect of this invention, the silicate mineral is olivine. In accordance with this invention, there is provided a carbon dioxide sequestering air filter media comprising a cloth made out of carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In another aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers. In yet another aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate and silicate mineral fibers. In a further aspect of this invention, the particle size of the silicate minerals is between 1.0 mm and 0.01 mm. In another aspect of this invention, the air filter media retains almost all particles of greater than 5μ size. In accordance with this invention, there is provided a carbon dioxide sequestering air filter, arranged so that air flowing through the filter passes through a layer of carbon dioxide sequestering media and a layer of air filter media. In accordance with this invention, there is provided a method of sequestering carbon dioxide, comprising: inserting an air filter comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals, into an air duct; and forcing air through the air filter. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In another aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers.|Turning to FIG. 2, there is provided regular air filter media 20 .| (US11426695)|CARBON DIOXIDE(100,121)|SEQUESTERING MEDIA(100,56)|AIR FILTER MEDIA(100,55)|AIR FILTER(100,15)|MEDIA(100,10)|CARBON DIOXIDE SEQUESTRATION(100,2)|CARBON DIOXIDE SEQUESTERING MEDIA(77,55)|SILICATE MINERAL UNCOATED FIBER(57,4)|UNCOATED FIBER(55,6)|UNCOATED SILICATE MINERAL(46,3)|SILICATE MINERAL(42,54)|WOVEN YARN(36,3)|SILICATE MINERAL FIBER(32,11)|FOSTERITE(31,3)|WOVEN SUBSTRATE(31,2)|OLIVINE(30,12)|FAYALITE(26,4)|SEQUESTERING FILTER MEDIA(24,3)|YARN(22,17)|MINERAL(22,5)|SILICATE MINERAL DUST(20,1)|CARBON DIOXIDE SEQUESTERING FILTER(18,2)|ENERGY INTENSIVE(17,1)|CLOTH(15,10)|DEPLOYMENT(13,1)|DUCTWORK(11,2)|SEQUESTERING AIR FILTER MEDIA(10,20)|SEQUESTERING AIR FILTER(10,8)|BONDING AGENT(10,4)|SOIL TEMPERATURE(9,2)|INDUSTRIAL BUILDING(8,2)|SILICATE MINERAL PARTICLE(7,10)|GREENHOUSE GAS(7,2)|AIR DUCT(6,1)|AUTOMOBILE CABIN VENTILATION(6,1)|PARTICLE SIZE(5,5)|EARTH ATMOSPHERE(4,3)|GREENHOUSE EFFECT(4,2)|BILL FREEDMAN(4,1)|CRUSHED OLIVINE(4,1)|SPINNING MOLTEN SILICATE MINERAL(4,1)|CARBON DIOXIDE SEQUESTERING FIBER(3,2)|CHEAP TOOL RO(3,1)|EARTH CRUST(3,1)|INTERMIXING THREAD(3,1)|KITCHEN EXHAUST FAN(3,1)|OLIVINE COATED SUBSTRATE(3,1)|SEPARATOR CONTEXT(3,1)|SILICATE MINERAL NATURAL WEATHERING(3,1)|SPINNING SILICATE MINERAL(3,1)|WIDESPREAD CONSUMER(3,1)|ARTIFICIAL MOVING AIR PATH(2,3)|CARBON DIOXIDE EMISSION(2,2)|SHORT THREAD(2,2)|CARBON DIOXIDE NATURAL WEATHERING(2,1)|COARSE FILTER(2,1)|CONTEXT DISCUSSION(2,1)|COVER THREAD(2,1)|COVERED STRING(2,1)|DUCTWORK EXPENSIVE REBUILDING(2,1)|INDUSTRIAL APPLICATION(2,1)|SEQUESTERING CARBON DIOXIDE(2,1)|WOOL FIBER(2,1)|BASALT(1,1)|CARBON DIOXIDE ABSORPTION(1,1)|CIRCULAR SUBSTRATE(1,1)|DIRT AIR(1,1)|DUCTWORK SIZE(1,1)||(US20200114310)|METHANEDIONE SEQUESTERING MEDIA(100,62)|SEQUESTERING MEDIA(100,62)|AIR FILTER MEDIA(100,61)|METHANEDIONE(100,58)|SEQUESTERING AIR FILTER MEDIA(100,36)|AIR FILTER(100,17)|MEDIA(100,10)|FILTER(100,9)|METHANEDIONE SEQUESTERING AIR FILTER(100,9)|SEQUESTERING AIR FILTER(100,9)|AIR(100,7)|METHANEDIONE SEQUESTERING MEDIA LAYER(100,5)|AIR FILTER MEDIA LAYER(100,2)|METHANEDIONE SEQUESTRATION(100,2)|SILICATE MINERAL(22,57)|SILICATE MINERAL FIBER(22,16)|METHANEDIONE SEQUESTERING FILTER MEDIA(19,3)|SILICATE MINERAL DUST(10,1)|OLIVINE(8,8)|ENERGY INTENSIVE(8,1)|DUCTWORK(7,1)|CLOTH(6,7)|DEPLOYMENT(6,1)|SILICATE MINERAL PARTICLE(4,10)|AIR DUCT(4,2)|GREENHOUSE GAS(4,2)|INDUSTRIAL BUILDING(4,2)|METHANEDIONE SEQUESTERING FIBER(4,2)|METHANEDIONE SEQUESTERING MEDIA FIBER(4,2)|SOIL TEMPERATURE(4,2)|PARTICLE SIZE(3,7)|METHANEDIONE EMISSION(3,2)|METHANEDIONE SEQUESTERING MEDIA ILLUSTRATION(3,2)|AUTOMOBILE CABIN VENTILATION(3,1)|YARN(2,12)|AWARE FIBER(2,5)|EARTH ATMOSPHERE(2,3)|GREENHOUSE EFFECT(2,2)|AWARE ROCK WOOL FIBER(2,1)|BILL FREEDMAN(2,1)|CRUSHED OLIVINE(2,1)|METHANEDIONE ABSORPTION(2,1)|METHANEDIONE NATURAL WEATHERING(2,1)|SEQUESTERING METHANEDIONE(2,1)|SPINNING MOLTEN SILICATE MINERAL(2,1)|STRING(1,4)|ARTIFICIAL MOVING AIR PATH(1,3)|SHORT THREAD(1,2)|AWARE SHORT PIECE(1,1)|BASALT(1,1)|CHEAP TOOL RO(1,1)|CIRCULAR SUBSTRATE(1,1)|COARSE FILTER(1,1)|CONTEXT DISCUSSION(1,1)|DIRT AIR(1,1)|DUCTWORK EXPENSIVE REBUILDING(1,1)|EARTH CRUST(1,1)|INDUSTRIAL APPLICATION(1,1)|INTERMIXING THREAD(1,1)|KITCHEN EXHAUST FAN(1,1)|METHANEDIONE FILTERING MEDIUM(1,1)|METHANEDIONE SEQUESTERING FILTERING MEDIUM(1,1)|OLIVINE COATED SUBSTRATE(1,1)|SEPARATOR CONTEXT(1,1)|SILICATE MINERAL NATURAL WEATHERING(1,1)|SPINNING SILICATE MINERAL(1,1)|WIDESPREAD CONSUMER(1,1)||(US20190321777)|SEQUESTERING FILTER(100,15)|CRUSHED OLIVINE(100,8)|SUBSTRATE(100,8)|METHANEDIONE SEQUESTERING FILTER(100,5)|TWO PIECE(100,4)|UNOBSTRUCTED CONTAINMENT STRUCTURE(100,4)|FILTER MEDIA(100,3)|FILTER MEDIA TWO PIECE(100,3)|CRUSHED OLIVINE CONTAINMENT(100,2)|CRUSHED OLIVINE BONDING(100,1)|METHANEDIONE(25,31)|EARTH ATMOSPHERE(20,4)|SILICATE MINERAL ENHANCED WEATHERING(17,1)|SILICATE MINERAL(16,13)|ENERGY INTENSIVE(16,1)|OLIVINE(15,21)|ENHANCED WEATHERING(10,7)|SEQUESTERING METHANEDIONE(8,3)|SOIL TEMPERATURE(8,2)|DIRT FILTERING AIR FILTER(8,1)|GREENHOUSE GAS(6,3)|COARSELY CRUSHED OLIVINE(6,1)|CARBON DIOXIDE SEQUESTERING FILTER(5,10)|METHANEDIONE EMISSION(5,2)|AUTOMOBILE CABIN VENTILATION(5,1)|METHANEDIONE NATURAL WEATHERING(5,1)|GREENHOUSE EFFECT(4,2)|BILL FREEDMAN(4,1)|OLIVINE LITER(4,1)|ARTIFICIAL MOVING AIR PATH(3,7)|ARTIFICIAL MOVING AIR DUCTWORK(3,2)|FILTER PACK(3,2)|EARTH CRUST(3,1)|ENVIROMENTAL BENEFIT(3,1)|OLIVINE MINERAL(3,1)|SILICATE MINERAL OLIVINE(3,1)|ABUNDANCE(2,2)|DUCTWORK OUTPUT(2,1)|KITCHEN EXHAUST FAN(2,1)|OIL LITTER(2,1)|SIMPLIFY INSTALLATION(2,1)| (US11426695)|What is claimed is:|1. An air filter media comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media comprises a woven substrate and uncoated fibers of a silicate mineral,| wherein the uncoated fibers are woven into the substrate;| wherein the silicate mineral is at least one mineral selected from the group consisting of olivine, fayalite, fosterite, and serpentine; and| wherein the carbon dioxide sequestering media is air-porous.|2. The air filter media of claim 1, wherein the uncoated fibers of the silicate mineral have varying lengths.|3. The air filter media of claim 2,| wherein the carbon dioxide sequestering media media comprises a cloth, the cloth comprising a plurality of woven yarns;| wherein each of the woven yarns comprises a plurality of the uncoated fibers twisted together.|4. The air filter media of claim 1, where the silicate mineral comprises olivine.|5. The air filter media of claim 4, wherein the uncoated fibers of the silicate mineral have varying lengths.|6. An air filter media comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media comprises a woven substrate and a plurality of yarns,| wherein each yarn comprises at least two uncoated fibers of a silicate mineral twisted together;| wherein the plurality of yarns are woven into the substrate;| wherein the silicate mineral is at least one mineral selected from the group consisting of olivine, fayalite, fosterite, and serpentine; and| wherein the carbon dioxide sequestering media is air-porous.|7. An air filter media comprising:| an air-porous first substrate,| an air filter media containing carbon dioxide sequestering media,| wherein the carbon dioxide sequestering media incorporates an uncoated silicate mineral,| wherein the silicate mineral is at least one mineral selected from the group consisting of olivine, fayalite, fosterite, and serpentine; and| a bonding agent;| wherein the bonding agent bonds the uncoated silicate minerals to the air-porous first substrate.|8. The air filter media of claim 7, wherein the uncoated silicate mineral comprises olivine.|9. The air filter media of claim 7, wherein the first substrate comprises a thread.|10. The air filter media of claim 7,| wherein the first substrate comprises a yarn;| wherein the yarn comprises at least two threads twisted together.|11. The air filter media of claim 7,| wherein the first substrate comprises a cloth, the cloth comprising a plurality of woven yarns. (US11426695)|BACKGROUND OF THE INVENTION|[0001] Carbon dioxide, along with other greenhouse gases, are responsible for the greenhouse effect, which is causing the Earth's temperature to rise. Reducing greenhouse gases would, in theory, reduce the greenhouse effect and stop the rise in the Earth's temperature. Carbon dioxide is the second most important greenhouse gas and it is controllable. Current efforts to control the amount of carbon dioxide in the atmosphere include the reduction in the use of fossil fuels, sequestering carbon dioxide at the site where large amounts of fossil fuels are consumed in industrial processes, and sequestering some of the carbon dioxide already in the atmosphere.|[0002] Current carbon sequestering involves expensive, energy consuming large scale systems that process flue gases and must be installed at the site of the carbon dioxide emission. The carbon dioxide emissions at the site of the large scale sequestering is generally 10% or more of the flue gases. The high amount of carbon dioxide in industrial emissions justifies the money spent to sequester the carbon dioxide because there is lots of it (carbon dioxide) to sequester at one location. See Bill Freedman and Todd Keith, “Planting trees for carbon credits: a discussion of context, issues, feasibility, and environmental benefits”, 4(2) Environmental Review (1996) pp 100-110.|[0003] Sequestering carbon dioxide from the atmosphere, for widespread consumer use, needs a different approach. The concentration of carbon dioxide in the atmosphere is about 0.04%. Large scale sequestering of carbon dioxide from the Earth's atmosphere is not practical due to the low concentrations. A proposal is to crush and spread the mineral olivine over the surface of the Earth and in the oceans. The mineral olivine and other silicate minerals sequester carbon dioxide through natural weathering when exposed to the atmosphere. See R. D. Schuiling and P. Krijgsman, “Enhanced Weathering: An Effective and Cheap Tool ro Sequester CO2”, 74 Climatic Change pp 349-354 (2006). The proposal to spread olivine or other silicate minerals on the earth would be energy intensive expensive, and time consuming. The natural weathering process is slow in sequestering carbon dioxide because the air movement over the silicate mineral is provided by nature and is variable or non-existence at times. It is known to create an olivine coated substrate in the context of separators for batteries (not the sequestering of carbon dioxide): see U.S. Pat. No. 3,861,963A of Afrance.|BRIEF SUMMARY OF THE INVENTION|[0004] This approach sequesters small amounts of carbon dioxide at a large number of locations. This invention is focused on the use of silicate minerals as a sequestering material, in that the path of artificial moving air to sequester the low concentration of carbon dioxide from the Earth's atmosphere. All silicate minerals that sequester carbon dioxide can be considered useable by this process where practical. A preferred mineral for use with this invention is olivine as this silicate mineral is abundant in the Earth's crust. This invention will enhance the natural weathering of the silicate mineral to speed up the sequestering of carbon dioxide by using the silicate material as a filter, in the path of artificial moving air. This invention is low cost, small scale (although it can be scaled up), so that even homeowners can participate in the sequestering of carbon dioxide. Use of this invention will result in small amounts of carbon sequestering at large numbers of locations.|[0005] Carbon dioxide sequestering media can be created by bonding a silicate mineral onto a substrate such as a thread. The substrate can then be cut as desired to create small pieces of carbon dioxide sequestering media. In a second embodiment, carbon dioxide sequestering media can also be created by spinning silicate mineral into rock wool fibers. This media can be used|[0006] Carbon dioxide sequestering air filter media can be created using the carbon dioxide sequestering media, which can then be used instead of traditional air filtering media in home and commercial applications. Carbon dioxide sequestering air filter media can be created, in a first embodiment, by mixing short pieces of a silicate mineral bonded to a substrate such as a thread with regular air filter media fibers. In a second embodiment, the silicate minerals spun into fibers are used on their own to form a Carbon dioxide sequestering air filter media, optionally mixed with silicate minerals bonded to a substrate such as a thread. In a third embodiment, the silicate minerals spun into fibers are mixed with air filter media fibers to form a carbon dioxide sequestering air filter media.|[0007] In accordance with the invention, there is provided a carbon dioxide sequestering air filter media comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In a further aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers. In a further aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate and silicate mineral fibers. In another aspect of this invention, the particle size of the silicate minerals is between 1.0 mm and 0.01 mm. In a further aspect of this invention, the silicate mineral is olivine.|[0008] In accordance with this invention, there is provided a carbon dioxide sequestering air filter media comprising a cloth made out of carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In another aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers. In yet another aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate and silicate mineral fibers. In a further aspect of this invention, the particle size of the silicate minerals is between 1.0 mm and 0.01 mm. In another aspect of this invention, the air filter media retains almost all particles of greater than 5μ size.|[0009] In accordance with this invention, there is provided a carbon dioxide sequestering air filter, arranged so that air flowing through the filter passes through a layer of carbon dioxide sequestering media and a layer of air filter media.|[0010] In accordance with this invention, there is provided a method of sequestering carbon dioxide, comprising: inserting an air filter comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals, into an air duct; and forcing air through the air filter. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In another aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers.|(US11426695)|DESCRIPTION OF THE FIGURES|[0011] In order to better understand various exemplary embodiments, reference is made to the accompanying drawings, wherein:|[0012] FIG. 1A a cross section of a round substrate with silicate minerals bonded to a thread;|[0013] FIG. 1B is an illustration of a side view of silicate minerals bonded to threads substrate to form a first embodiment of carbon dioxide sequestering media;|[0014] FIG. 2 is an illustration of carbon dioxide sequestering media mixed into traditional air filter media;|[0015] FIG. 3 is an illustration of carbon dioxide sequestering media woven to form a cloth that is a carbon dioxide sequestering air filter media; and|[0016] FIG. 4 shows threads or fibers of carbon dioxide sequestering media spun or twisted to form a yarn.|(US11426695)|DETAILED DESCRIPTION OF THE INVENTION|[0017] This invention is media for sequestering carbon dioxide from the Earth's atmosphere using enhanced weathering of silicate mineral particles, or the chemical absorption of carbon dioxide by silicate mineral particles. Such media can also include air filtering media that also sequesters carbon dioxide. These media are particularly useful for deployment in ductworks in residential, commercial and industrial buildings.|[0018] Examples of silicate minerals include basalt, wollastonite, fayalite, forsterite, olivine, and serpentine. Olivine is one of the most common minerals on earth by volume, and is widely available. Olivine is a preferred silicate mineral as it reacts easily with carbon dioxide from the atmosphere.|[0019] In this application, the term “air filter” means the air filter that cleans the air of dirt.|[0020] Carbon dioxide sequestering media can be created, in a first embodiment, by bonding a silicate material to a substrate. The substrate can have a round, square, or rectangular cross section or any other practical cross-section that is useable as described here. The silicate material is crushed to a particle size of of 0.01 to 1.0 mm, and preferably 0.010 mm. The bonding is done in such a way that when the silicate mineral particles are bonded to the substrate, the silicate mineral particles stand proud of the surface of the substrate. The substrate with the bonding agent and the silicate mineral particles can be rigid or flexible.|[0021] FIGS. 1A and 1B illustrate silicate minerals bonded to a string or thread substrate to form an embodiment of carbon dioxide sequestering media. Turning to FIG. 1A, there are silicate mineral particles 2 bonded with bonding agent 4 to strings or threads 6, which together form an embodiment of a carbon dioxide sequestering media. Turning to FIG. 1B, it may be seen that the spacing of the silicate mineral particles 2 may vary. In a preferred embodiment, the silicate mineral particles 2 cover most of the length of thread 6, forming a covered thread 8 as seen in FIG. 1B The method of bonding may make the covered strings or threads 8 rigid, or may leave the strings or threads 8 flexible. The threads 6 may be long or short; longer threads may be woven to form a substrate or may be woven with other materials, such as air filter materials. Shorter threads may be intermingled within other media.|[0022] The silicate mineral particles are sized to a diameter between 0.01 mm to 1 mm. The silicate mineral particles may be a mixture of silicate minerals, or may be just one silicate mineral. In a preferred embodiment, the silicate mineral includes, or is entirely comprised of, olivine.|[0023] Carbon dioxide sequestering filter media can also be made without a substrate by spinning molten silicate minerals into fibers, similar to the processes used when mineral wool is manufactured. Such fibers typically have a diameter of 2-6 micrometers. The fibers created in this manner may be long or short; longer threads may be woven to form a substrate or may be woven with other materials, such as air filter materials. Shorter threads may be intermingled within other media.|[0024] The carbon dioxide filtering media may be placed in the path of artificial moving air, ideally at the position where the air temperature is the highest. The artificial moving air is at the pressure and temperature provided by the ventilation system (at ambient pressure and ambient temperature).|[0025] The artificial moving air is provided by many sources such as central heating/cooling systems and ventilation systems that are present in residential, commercial and industrial buildings. Other minor sources of artificial moving air are vacuum cleaners, automobile cabin ventilation, and kitchen exhaust fans. There are many variables in artificial moving air systems including the speed of the air flow, the volume of the air flow, and the size of the ductwork. These variables will determine the size of the crushed olivine, the substrate size, and the construction of the substrate.|[0026] Threads or fibers of carbon dioxide sequestering media may be spun to form a yarn. FIG. 4 shows spinning at least two carbon dioxide sequestering fibers or threads to form a yarn. Turning to FIG. 4, two carbon dioxide sequestering fibers or threads 40 are shown being twisted or spun to form a yarn 42. A person skilled in the art would appreciate that such yarn could be made from more than two fibers, could be made entirely from silicate mineral fibers, or entirely from threads with silicate minerals bonded to the threads or from any combination of silicate mineral fibers and threads bonded to silicate minerals.|[0027] The carbon dioxide sequestering media, whether silicate mineral bonded to a substrate or spun silicate mineral fibers, or a combination of these, or a yarn, may be suspended within a frame and inserted into ductwork such that the silicate minerals are exposed to, and absorb carbon dioxide from, the passing air. The frame and carbon dioxide sequestering media may be replaced periodically. This approach will, however, require ductwork to be either built or re-built to accommodate the frame and silicate minerals.|[0028] This can be avoided by using the carbon dioxide sequestering media to create carbon dioxide sequestering air filter media. Carbon dioxide sequestering air filter media can be used instead of traditional air filter media to create a carbon dioxide sequestering air filter, which can be used like a traditional air filter in residential, commercial and industrial settings without requiring expensive re-building of ductwork.|[0029] Carbon dioxide sequestering air filter media can be created, in a first embodiment, by mixing pieces of carbon dioxide sequestering media with regular air filters. Turning to FIG. 2, there is provided regular air filter media 20. Interspersed or mixed into the regular air filter media 20 are carbon dioxide sequestering media 22. The carbon dioxide sequestering media 22 may be silicate minerals bonded to a substrate, or may be silicate mineral fibers, or a yarn as described above. In a preferred embodiment, the carbon dioxide sequestering media 22 is silicate minerals bonded to a thread. In another preferred embodiment, the carbon dioxide sequestering media 22 is silicate minerals bonded to a thread, and the media is cut into short pieces and is then mixed with the air filter media. In another preferred embodiment, the carbon dioxide sequestering media 22 is silicate minerals bonded to a thread, and the thread is woven through the air filter media. In another preferred embodiment, the carbon dioxide sequestering media 22 is a yarn, and the yarn is woven through the air filter media. The carbon dioxide sequestering air filter media may then be used to create a carbon dioxide sequestering air filter by using the dioxide sequestering air filter media in place of traditional air filter media in nan air filter. The resulting carbon dioxide sequestering air filter may then be used in the same manner as a traditional air filter.|[0030] In a second embodiment, the carbon dioxide sequestering media is used on its own to form a carbon dioxide sequestering air filter media. Turning to FIG. 3, carbon dioxide sequestering media 30 is interwoven with carbon dioxide sequestering media 32 to create a carbon dioxide sequestering air filter media 34. Carbon dioxide sequestering air filter media 34 may be described as a cloth. Carbon dioxide sequestering media 30 and 32 may be created from either silicate minerals bonded to a substrate or silicate minerals spun into fibers, or yarns as described above. Carbon dioxide sequestering air filter media 34 may be described as a cloth. Combinations and mixtures of either silicate minerals bonded to a substrate or silicate minerals spun into fibers may be used. In a preferred embodiment, by intermixing threads or strong substrates bonded with silicate mineral fibers, greater strength and rip-resistance may be imparted to yarns or cloths as described above when compared to yarns or cloths composed entirely of silicate mineral fibers. Carbon dioxide sequestering air filter media 34 may be placed in a frame to create a carbon dioxide sequestering air filter, which may be used in place of traditional air filters.|[0031] Similar to traditional air filter media, carbon dioxide sequestering air filter media 34 must be air-porous and allow air to flow through without creating significant back-pressure problems, while the pores are sized to allow the carbon dioxide sequestering air filter media 34 to filter dirt from the air. Generally, the pores in the carbon dioxide sequestering air filter media can have ranges in performance: under the European standard EN779, these can range from Class G1: 65% performance with approaching 100% retention of particulate size greater than 5μ (coarse filters) to Class U17 with 99.999995% performance with approaching 100% retention of particulate size greater than 0.3μ (ULPA).|[0032] In another embodiment, a carbon dioxide sequestering air filter is constructed such that air flowing through the air filter passes through a layer of traditional air filter media and through a layer of carbon dioxide sequestering media. The air flowing through the air filter may pass first through a layer of traditional air filter media and then through a layer of carbon dioxide sequestering media, or air flowing through the air filter passes through a layer of carbon dioxide sequestering media and then a layer of traditional air filter media. The air filter may also be constructed so that the air passes through multiple layers of either traditional air filter media and/or carbon dioxide sequestering media.|[0033] For all embodiments of a carbon dioxide sequestering air filter, since there is the possibility of damage to the filter allowing dust to be created from the silicate minerals, it is desirable from a safety point of view for the filter to be constructed so the air flows through a traditional air filter media as a last step before leaving the filter, and for the traditional air filter in this last step to be sized so as to control any escape of silicate mineral dust or particles.|[0034] When the carbon dioxide sequestering filtering media is used as part of an air filter (thus creating a carbon dioxide sequestering air filter), it can be used for residential, commercial or industrial installations. The media created here can be used with air filter media or to replace the air filter media currently used. (US11426695)|BACKGROUND OF THE INVENTION|[0001] Carbon dioxide, along with other greenhouse gases, are responsible for the greenhouse effect, which is causing the Earth's temperature to rise. Reducing greenhouse gases would, in theory, reduce the greenhouse effect and stop the rise in the Earth's temperature. Carbon dioxide is the second most important greenhouse gas and it is controllable. Current efforts to control the amount of carbon dioxide in the atmosphere include the reduction in the use of fossil fuels, sequestering carbon dioxide at the site where large amounts of fossil fuels are consumed in industrial processes, and sequestering some of the carbon dioxide already in the atmosphere.|[0002] Current carbon sequestering involves expensive, energy consuming large scale systems that process flue gases and must be installed at the site of the carbon dioxide emission. The carbon dioxide emissions at the site of the large scale sequestering is generally 10% or more of the flue gases. The high amount of carbon dioxide in industrial emissions justifies the money spent to sequester the carbon dioxide because there is lots of it (carbon dioxide) to sequester at one location. See Bill Freedman and Todd Keith, “Planting trees for carbon credits: a discussion of context, issues, feasibility, and environmental benefits”, 4(2) Environmental Review (1996) pp 100-110.|[0003] Sequestering carbon dioxide from the atmosphere, for widespread consumer use, needs a different approach. The concentration of carbon dioxide in the atmosphere is about 0.04%. Large scale sequestering of carbon dioxide from the Earth's atmosphere is not practical due to the low concentrations. A proposal is to crush and spread the mineral olivine over the surface of the Earth and in the oceans. The mineral olivine and other silicate minerals sequester carbon dioxide through natural weathering when exposed to the atmosphere. See R. D. Schuiling and P. Krijgsman, “Enhanced Weathering: An Effective and Cheap Tool ro Sequester CO2”, 74 Climatic Change pp 349-354 (2006). The proposal to spread olivine or other silicate minerals on the earth would be energy intensive expensive, and time consuming. The natural weathering process is slow in sequestering carbon dioxide because the air movement over the silicate mineral is provided by nature and is variable or non-existence at times. It is known to create an olivine coated substrate in the context of separators for batteries (not the sequestering of carbon dioxide): see U.S. Pat. No. 3,861,963A of Afrance.|BRIEF SUMMARY OF THE INVENTION|[0004] This approach sequesters small amounts of carbon dioxide at a large number of locations. This invention is focused on the use of silicate minerals as a sequestering material, in that the path of artificial moving air to sequester the low concentration of carbon dioxide from the Earth's atmosphere. All silicate minerals that sequester carbon dioxide can be considered useable by this process where practical. A preferred mineral for use with this invention is olivine as this silicate mineral is abundant in the Earth's crust. This invention will enhance the natural weathering of the silicate mineral to speed up the sequestering of carbon dioxide by using the silicate material as a filter, in the path of artificial moving air. This invention is low cost, small scale (although it can be scaled up), so that even homeowners can participate in the sequestering of carbon dioxide. Use of this invention will result in small amounts of carbon sequestering at large numbers of locations.|[0005] Carbon dioxide sequestering media can be created by bonding a silicate mineral onto a substrate such as a thread. The substrate can then be cut as desired to create small pieces of carbon dioxide sequestering media. In a second embodiment, carbon dioxide sequestering media can also be created by spinning silicate mineral into rock wool fibers. This media can be used|[0006] Carbon dioxide sequestering air filter media can be created using the carbon dioxide sequestering media, which can then be used instead of traditional air filtering media in home and commercial applications. Carbon dioxide sequestering air filter media can be created, in a first embodiment, by mixing short pieces of a silicate mineral bonded to a substrate such as a thread with regular air filter media fibers. In a second embodiment, the silicate minerals spun into fibers are used on their own to form a Carbon dioxide sequestering air filter media, optionally mixed with silicate minerals bonded to a substrate such as a thread. In a third embodiment, the silicate minerals spun into fibers are mixed with air filter media fibers to form a carbon dioxide sequestering air filter media.|[0007] In accordance with the invention, there is provided a carbon dioxide sequestering air filter media comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In a further aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers. In a further aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate and silicate mineral fibers. In another aspect of this invention, the particle size of the silicate minerals is between 1.0 mm and 0.01 mm. In a further aspect of this invention, the silicate mineral is olivine.|[0008] In accordance with this invention, there is provided a carbon dioxide sequestering air filter media comprising a cloth made out of carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In another aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers. In yet another aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate and silicate mineral fibers. In a further aspect of this invention, the particle size of the silicate minerals is between 1.0 mm and 0.01 mm. In another aspect of this invention, the air filter media retains almost all particles of greater than 5μ size.|[0009] In accordance with this invention, there is provided a carbon dioxide sequestering air filter, arranged so that air flowing through the filter passes through a layer of carbon dioxide sequestering media and a layer of air filter media.|[0010] In accordance with this invention, there is provided a method of sequestering carbon dioxide, comprising: inserting an air filter comprising air filter media containing carbon dioxide sequestering media, wherein the carbon dioxide sequestering media incorporates silicate minerals, into an air duct; and forcing air through the air filter. In an aspect of this invention, the carbon dioxide sequestering media comprises silicate minerals bonded to a substrate. In another aspect of this invention, the substrate is a thread. In another aspect of this invention, the carbon dioxide sequestering media comprises silicate mineral fibers.|(US11426695)|DESCRIPTION OF THE FIGURES|[0011] In order to better understand various exemplary embodiments, reference is made to the accompanying drawings, wherein:|[0012] FIG. 1A a cross section of a round substrate with silicate minerals bonded to a thread;|[0013] FIG. 1B is an illustration of a side view of silicate minerals bonded to threads substrate to form a first embodiment of carbon dioxide sequestering media;|[0014] FIG. 2 is an illustration of carbon dioxide sequestering media mixed into traditional air filter media;|[0015] FIG. 3 is an illustration of carbon dioxide sequestering media woven to form a cloth that is a carbon dioxide sequestering air filter media; and|[0016] FIG. 4 shows threads or fibers of carbon dioxide sequestering media spun or twisted to form a yarn.|(US11426695)|DETAILED DESCRIPTION OF THE INVENTION|[0017] This invention is media for sequestering carbon dioxide from the Earth's atmosphere using enhanced weathering of silicate mineral particles, or the chemical absorption of carbon dioxide by silicate mineral particles. Such media can also include air filtering media that also sequesters carbon dioxide. These media are particularly useful for deployment in ductworks in residential, commercial and industrial buildings.|[0018] Examples of silicate minerals include basalt, wollastonite, fayalite, forsterite, olivine, and serpentine. Olivine is one of the most common minerals on earth by volume, and is widely available. Olivine is a preferred silicate mineral as it reacts easily with carbon dioxide from the atmosphere.|[0019] In this application, the term “air filter” means the air filter that cleans the air of dirt.|[0020] Carbon dioxide sequestering media can be created, in a first embodiment, by bonding a silicate material to a substrate. The substrate can have a round, square, or rectangular cross section or any other practical cross-section that is useable as described here. The silicate material is crushed to a particle size of of 0.01 to 1.0 mm, and preferably 0.010 mm. The bonding is done in such a way that when the silicate mineral particles are bonded to the substrate, the silicate mineral particles stand proud of the surface of the substrate. The substrate with the bonding agent and the silicate mineral particles can be rigid or flexible.|[0021] FIGS. 1A and 1B illustrate silicate minerals bonded to a string or thread substrate to form an embodiment of carbon dioxide sequestering media. Turning to FIG. 1A, there are silicate mineral particles 2 bonded with bonding agent 4 to strings or threads 6, which together form an embodiment of a carbon dioxide sequestering media. Turning to FIG. 1B, it may be seen that the spacing of the silicate mineral particles 2 may vary. In a preferred embodiment, the silicate mineral particles 2 cover most of the length of thread 6, forming a covered thread 8 as seen in FIG. 1B The method of bonding may make the covered strings or threads 8 rigid, or may leave the strings or threads 8 flexible. The threads 6 may be long or short; longer threads may be woven to form a substrate or may be woven with other materials, such as air filter materials. Shorter threads may be intermingled within other media.|[0022] The silicate mineral particles are sized to a diameter between 0.01 mm to 1 mm. The silicate mineral particles may be a mixture of silicate minerals, or may be just one silicate mineral. In a preferred embodiment, the silicate mineral includes, or is entirely comprised of, olivine.|[0023] Carbon dioxide sequestering filter media can also be made without a substrate by spinning molten silicate minerals into fibers, similar to the processes used when mineral wool is manufactured. Such fibers typically have a diameter of 2-6 micrometers. The fibers created in this manner may be long or short; longer threads may be woven to form a substrate or may be woven with other materials, such as air filter materials. Shorter threads may be intermingled within other media.|[0024] The carbon dioxide filtering media may be placed in the path of artificial moving air, ideally at the position where the air temperature is the highest. The artificial moving air is at the pressure and temperature provided by the ventilation system (at ambient pressure and ambient temperature).|[0025] The artificial moving air is provided by many sources such as central heating/cooling systems and ventilation systems that are present in residential, commercial and industrial buildings. Other minor sources of artificial moving air are vacuum cleaners, automobile cabin ventilation, and kitchen exhaust fans. There are many variables in artificial moving air systems including the speed of the air flow, the volume of the air flow, and the size of the ductwork. These variables will determine the size of the crushed olivine, the substrate size, and the construction of the substrate.|[0026] Threads or fibers of carbon dioxide sequestering media may be spun to form a yarn. FIG. 4 shows spinning at least two carbon dioxide sequestering fibers or threads to form a yarn. Turning to FIG. 4, two carbon dioxide sequestering fibers or threads 40 are shown being twisted or spun to form a yarn 42. A person skilled in the art would appreciate that such yarn could be made from more than two fibers, could be made entirely from silicate mineral fibers, or entirely from threads with silicate minerals bonded to the threads or from any combination of silicate mineral fibers and threads bonded to silicate minerals.|[0027] The carbon dioxide sequestering media, whether silicate mineral bonded to a substrate or spun silicate mineral fibers, or a combination of these, or a yarn, may be suspended within a frame and inserted into ductwork such that the silicate minerals are exposed to, and absorb carbon dioxide from, the passing air. The frame and carbon dioxide sequestering media may be replaced periodically. This approach will, however, require ductwork to be either built or re-built to accommodate the frame and silicate minerals.|[0028] This can be avoided by using the carbon dioxide sequestering media to create carbon dioxide sequestering air filter media. Carbon dioxide sequestering air filter media can be used instead of traditional air filter media to create a carbon dioxide sequestering air filter, which can be used like a traditional air filter in residential, commercial and industrial settings without requiring expensive re-building of ductwork.|[0029] Carbon dioxide sequestering air filter media can be created, in a first embodiment, by mixing pieces of carbon dioxide sequestering media with regular air filters. Turning to FIG. 2, there is provided regular air filter media 20. Interspersed or mixed into the regular air filter media 20 are carbon dioxide sequestering media 22. The carbon dioxide sequestering media 22 may be silicate minerals bonded to a substrate, or may be silicate mineral fibers, or a yarn as described above. In a preferred embodiment, the carbon dioxide sequestering media 22 is silicate minerals bonded to a thread. In another preferred embodiment, the carbon dioxide sequestering media 22 is silicate minerals bonded to a thread, and the media is cut into short pieces and is then mixed with the air filter media. In another preferred embodiment, the carbon dioxide sequestering media 22 is silicate minerals bonded to a thread, and the thread is woven through the air filter media. In another preferred embodiment, the carbon dioxide sequestering media 22 is a yarn, and the yarn is woven through the air filter media. The carbon dioxide sequestering air filter media may then be used to create a carbon dioxide sequestering air filter by using the dioxide sequestering air filter media in place of traditional air filter media in nan air filter. The resulting carbon dioxide sequestering air filter may then be used in the same manner as a traditional air filter.|[0030] In a second embodiment, the carbon dioxide sequestering media is used on its own to form a carbon dioxide sequestering air filter media. Turning to FIG. 3, carbon dioxide sequestering media 30 is interwoven with carbon dioxide sequestering media 32 to create a carbon dioxide sequestering air filter media 34. Carbon dioxide sequestering air filter media 34 may be described as a cloth. Carbon dioxide sequestering media 30 and 32 may be created from either silicate minerals bonded to a substrate or silicate minerals spun into fibers, or yarns as described above. Carbon dioxide sequestering air filter media 34 may be described as a cloth. Combinations and mixtures of either silicate minerals bonded to a substrate or silicate minerals spun into fibers may be used. In a preferred embodiment, by intermixing threads or strong substrates bonded with silicate mineral fibers, greater strength and rip-resistance may be imparted to yarns or cloths as described above when compared to yarns or cloths composed entirely of silicate mineral fibers. Carbon dioxide sequestering air filter media 34 may be placed in a frame to create a carbon dioxide sequestering air filter, which may be used in place of traditional air filters.|[0031] Similar to traditional air filter media, carbon dioxide sequestering air filter media 34 must be air-porous and allow air to flow through without creating significant back-pressure problems, while the pores are sized to allow the carbon dioxide sequestering air filter media 34 to filter dirt from the air. Generally, the pores in the carbon dioxide sequestering air filter media can have ranges in performance: under the European standard EN779, these can range from Class G1: 65% performance with approaching 100% retention of particulate size greater than 5μ (coarse filters) to Class U17 with 99.999995% performance with approaching 100% retention of particulate size greater than 0.3μ (ULPA).|[0032] In another embodiment, a carbon dioxide sequestering air filter is constructed such that air flowing through the air filter passes through a layer of traditional air filter media and through a layer of carbon dioxide sequestering media. The air flowing through the air filter may pass first through a layer of traditional air filter media and then through a layer of carbon dioxide sequestering media, or air flowing through the air filter passes through a layer of carbon dioxide sequestering media and then a layer of traditional air filter media. The air filter may also be constructed so that the air passes through multiple layers of either traditional air filter media and/or carbon dioxide sequestering media.|[0033] For all embodiments of a carbon dioxide sequestering air filter, since there is the possibility of damage to the filter allowing dust to be created from the silicate minerals, it is desirable from a safety point of view for the filter to be constructed so the air flows through a traditional air filter media as a last step before leaving the filter, and for the traditional air filter in this last step to be sized so as to control any escape of silicate mineral dust or particles.|[0034] When the carbon dioxide sequestering filtering media is used as part of an air filter (thus creating a carbon dioxide sequestering air filter), it can be used for residential, commercial or industrial installations. The media created here can be used with air filter media or to replace the air filter media currently used. Family Number|(86377114)|86377114|Abstract|(US20190321777 A1)|Three methods of sequestering carbon dioxide from the atmosphere that uses an enhanced weathering effect of the mineral olivine. In method one, crushed olivine is bonded to a substrate to create a filter that sequesters carbon dioxide. Method two contains the crushed olivine between two pieces of filter media to create a filter that sequesters carbon dioxide. The third method uses an unobstructed containment structure loaded with crushed olivine to create a filter that sequesters carbon dioxide.|(US11426695 B2)|Filter media and filters for the sequestration of carbon dioxide are disclosed. The carbon dioxide sequestering filter media incorporate silicate minerals, and the carbon dioxide sequestering filters incorporate carbon dioxide sequestering filter media. Filters using only carbon dioxide sequestering media and filters combining carbon dioxide sequestering media with traditional air filter media are disclosed. The carbon dioxide sequestering filters may be used instead of traditional air filters in residential, commercial and industrial applications.|CPC codes|(US20190321777 A1)|B01D-053/02|B01D-053/62|B01D-2251/402|B01D-2253/106|B01D-2257/504|B01D-2258/06|(US11426695 B2)|B01D-053/02|B01D-053/04/07|B01D-053/62|B01D-053/82|B01D-2253/106|B01D-2253/25|B01D-2253/304|B01D-2253/34|B01D-2257/504|B01D-2257/50|B01D-2258/06|B01D-2259/4508|B01J-020/10|B01J-020/28/026|IPC codes|(US20190321777 A1)|B01D-053/62|(US11426695 B2)|B01D-053/04|B01D-053/62|B01D-053/82|B01J-020/10|Title|(US20190321777 A1)|Carbon dioxide sequestering filter|(US11426695 B2)|Media and air filters for carbon dioxide sequestration|(US20200114310 A1)|Media and air filters for carbon dioxide sequestration| Chemical engineering|Environmental technology B01D-053/02|B01D-053/04/07|B01D-053/62|B01D-053/82|B01D-2251/402|B01D-2253/106|B01D-2253/25|B01D-2253/304|B01D-2253/34|B01D-2257/50|B01D-2257/504|B01D-2258/06|B01D-2259/4508|B01J-020/10|B01J-020/28/026|Y02A-050/20|Y02C-020/40 B01D-053/02|B01D-053/04/07|B01D-053/62|B01D-053/82|B01D-2251/402|B01D-2253/106|B01D-2253/25|B01D-2253/304|B01D-2253/34|B01D-2257/50|B01D-2257/504|B01D-2258/06|B01D-2259/4508|B01J-020/10|B01J-020/28/026|Y02A-050/20|Y02C-020/40 B01D-053/04|B01D-053/62|B01D-053/82|B01J-020/10 B01D-053/04|B01D-053/62|B01D-053/82|B01J-020/10 WO2025196715|EP4208279|WO202248787|WO202177196|WO202564785|US20240367101|US20240307811|US12551845|CN114349533B|US11305230 WO2025196715 116103001 WHO=Examiner SELF=N CAT=X CAT=Y|EP4208279 92984336 WHO=Examiner SELF=N CAT=X CAT=I|WO202248787 92984336 WHO=Examiner SELF=N CAT=X CAT=I|WO202177196 93812748 WHO=Examiner SELF=N CAT=E CAT=X|WO202564785 113948303 WHO=Examiner SELF=N CAT=A|US20240367101 112020354 WHO=Examiner SELF=N CAT=103|US20240307811 92984336 WHO=Examiner SELF=N CAT=102 CAT=103|US12551845 112020354 WHO=Examiner SELF=N|CN114349533B 99640297 WHO=Examiner SELF=N|US11305230 99605938 WHO=Examiner SELF=N US20170007991|US20110006263|US3861963|US3861963|GB2081247|US3861963 US20170007991 64998322 WHO=Examiner SELF=N CAT=102|US20110006263 1016747 WHO=Examiner SELF=N CAT=102|US3861963 42239016 WHO=Examiner SELF=N CAT=102|US3861963 42239016 WHO=Examiner SELF=N CAT=102|GB2081247 18124639 WHO=Examiner SELF=N|US3861963 42239016 WHO=Applicant SELF=N US3861963; US20110006263; US20170007991; GB2081247; US3861963|US3861963 (US11426695)|Applicant references|-Schuiling, et al., “Enhanced Weathering: An Effective and Cheap Tool To Sequester CO2”, Climatic Change, 74: 349, pp. 349-354. (2006) (https://doi.org/10.1007/s10584-005-3485-y).|| GRANTED (US11426695)|GRANTED|(US20190321777)|LAPSED ALIVE (US11426695)|ALIVE|(US20190321777)|DEAD (US11426695)|LEGAL DETAILS FOR US11426695|Actual or expected expiration date=2038-04-23|Legal state=ALIVE|Status=GRANTED|Event publication date=2019-12-05|Event code=US/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=US US16704880|Application date=2019-12-05|Standardized application number=2019US-16704880|Event publication date=2019-12-05|Event code=US/EXMR|Event group=Administrative notifications|USPTO Examiner Name|PRIMARY EXAMINER:BERNS, DANIEL J|Event publication date=2019-12-05|Event code=US/ART|Event group=Administrative notifications|USPTO Art Group|ART=1736|Event publication date=2019-12-05|Event code=US/DK|Event group=Examination events|Attorney Docket Number|Docket Nbr: CLP 3031-CIP|Event publication date=2019-12-05|Event code=US/CUST|Event group=Examination events|Attorney/Agent Customer Number|Customer Nbr: 30868|Event publication date=2019-12-05|Event code=US/SMALL|Event group=Administrative notifications|Appl Has Filed a Verified Statement of Micro to Small Entity Status|Business Entity Status: Micro|Event publication date=2019-12-05|Event code=US/AIA|Event group=Administrative notifications|First Inventor File Indicated:|AIA=Yes|Event publication date=2019-12-05|Event code=US/IDS|Event group=Examination events OAI|Information Disclosure Statement Filed|Event publication date=2019-12-05|Event code=US/PTARDY|Event indicator=Pos|Event group=Examination events|Patent Term Adjustment - Ready for Examination|Event publication date=2019-12-05|Event code=US/ENT|Event group=Administrative notifications|Entity Status Set to Undiscounted|Event publication date=2020-01-02|Event code=US/SMALL|Event group=Administrative notifications|Appl Has Filed a Verified Statement of Micro to Small Entity Status|Event publication date=2020-01-06|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2020-01-07|Event code=US/APPFILEREC|Event group=Administrative notifications OAO|Filing Receipt|Event publication date=2020-04-16|Event code=US/A1|Event group=Examination events|Application published|Publication country=US|Publication number=US20200114310|Publication stage code=A1|Publication date=2020-04-16|Standardized publication number=US20200114310|Event publication date=2020-04-16|Event code=US/PGPUBN|Event indicator=Pos|Event group=Examination events OAO|PG-Pub Issue Notification|Event publication date=2020-11-18|Event code=US/CTNF|Event group=Examination events OA OAO|Non-Final Rejection|Event publication date=2020-11-23|Event code=US/112NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 112 - subject matter in claims not properly defined|RJD=2020-11-23|R4R=112b|RJST=non-final|Rejected claims 7|Event publication date=2020-11-23|Event code=US/112NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 112 - subject matter in claims not properly defined|RJD=2020-11-23|R4R=112d|RJST=non-final|Rejected claims 7; 7 may be infringed without necessarily also infringing claim 1, i.e. by employing only a single silicate mineral, claim 7|Event publication date=2020-11-23|Event code=US/102NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 102 - non-novel subject matter in claims|RJD=2020-11-23|R4R=102a|RJST=non-final|Rejected claims 1-4, 6-11, and 13-14; 4 and 11; 15|RJCT=US3861963|RJCT=US20110006263|Event publication date=2020-11-23|Event code=US/103NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 103 - obvious subject matter in claims|RJD=2020-11-23|R4R=103|RJST=non-final|Rejected claims 5 and 12|Event publication date=2021-02-23|Event code=US/AINEA|Event group=OAI Examination events|Informal or Non-Responsive Amendment after Examiner Action|Event publication date=2021-02-23|Event code=US/CTNFR|Event group=Examination events OAI|Response after Non-Final Action|Event publication date=2021-02-23|Event code=US/INVSUM|Event group=Examination events OAI INT|Interview Summary- Applicant Initiated|Event publication date=2021-02-23|Event code=US/EXIN|Event group=Examination events OAO INT|Examiner Interview Summary Record (PTOL - 413)|Event publication date=2021-06-02|Event code=US/INVSUM|Event group=Examination events OAI INT|Interview Summary- Applicant Initiated|Event publication date=2021-06-02|Event code=US/EXIN|Event group=Examination events OAO INT|Examiner Interview Summary Record (PTOL - 413)|Event publication date=2021-07-06|Event code=US/CTNFR|Event group=Examination events OAI|Response after Non-Final Action|Event publication date=2021-07-06|Event code=US/136G|Event group=OAO|Request for Extension of Time - Granted|Event publication date=2021-11-02|Event code=US/CTFR|Event group=Examination events OA OAO|Final Rejection|Event publication date=2021-11-05|Event code=US/112FR|Event indicator=Neg|Event group=Examination events|Final rejection reason 112 - subject matter in claims not properly defined|RJD=2021-11-05|R4R=112b|RJST=final|Rejected claims 40-58; 47|Event publication date=2021-11-05|Event code=US/101FR|Event indicator=Neg|Event group=Examination events|Final rejection reason 101 - subject matter not patentable|RJD=2021-11-05|R4R=101|RJST=final|Rejected claims 40-46, 50-55, and 58|Event publication date=2021-11-05|Event code=US/102FR|Event indicator=Neg|Event group=Examination events|Final rejection reason 102 - 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Ready for Examination|Event publication date=2018-06-28|Event code=US/RECEIPTUP|Event group=Administrative notifications OAO|Filing Receipt - Updated|Event publication date=2018-07-26|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2019-04-30|Event code=US/RESTREQ|Event group=Examination events Corrections OAO|Restriction/Election Requirement|Event publication date=2019-05-20|Event code=US/ELC|Event group=Examination events OAI|Response to Election / Restriction Filed|Event publication date=2019-06-03|Event code=US/CTNF|Event group=Examination events OA OAO|Non-Final Rejection|Event publication date=2019-06-05|Event code=US/112NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 112 - subject matter in claims not properly defined|RJD=2019-06-05|R4R=112b|RJST=non-final|Rejected claims 5-6|Event publication date=2019-06-05|Event code=US/112NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 112 - subject matter in claims not properly defined|RJD=2019-06-05|R4R=112d|RJST=non-final|Rejected claims 5; 1, i.e. by bonding a non-olivine silicate mineral (such as wollastonite) to a substrate, claim 5|Event publication date=2019-06-05|Event code=US/102NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 102 - non-novel subject matter in claims|RJD=2019-06-05|R4R=102a|RJST=non-final|Rejected claims 1; 1 and 6|RJCT=US3861963|Event publication date=2019-06-05|Event code=US/103NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 103 - obvious subject matter in claims|RJD=2019-06-05|R4R=103|RJST=non-final|Rejected claims 4-6; 5-6|Event publication date=2019-08-12|Event code=US/INVSUM|Event group=Examination events OAI INT|Interview Summary- Applicant Initiated|Event publication date=2019-09-13|Event code=US/POAC|Event group=Change of name or address|Change in Power of Attorney (May Include Associate POA)|Event publication date=2019-10-24|Event code=US/A1|Event group=Examination events|Application published|Publication country=US|Publication number=US20190321777|Publication stage code=A1|Publication date=2019-10-24|Standardized publication number=US20190321777|Event publication date=2019-10-24|Event code=US/PGPUBN|Event indicator=Pos|Event group=Examination events OAO|PG-Pub Issue Notification|Event publication date=2020-01-05|Event code=US/ABNOA|Event indicator=Neg|Event group=Event indicating Not In Force OAO|Abandoned -- Failure to Respond to an Office Action (US11426695)|US https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=HCOyy4WOJl7cRl63LisPHbaa7teVYIYQWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000020600512&ekey=2053&xpn=US11426695&kind=B2 https://data.uspto.gov/patent-file-wrapper/search/details/16704880/application-data https://permalink.orbit.com/RenderStaticFirstPage?XPN=GJW%252BTyVuImmtP5kNw6LZtTNfFPLuVTJ9KaVWfLIclG0%3D%26n%3D1&id=0&base=FAMPAT US (US11426695)|CA|(US20200114310)|CA|(US20190321777)|CA (US11426695)|NAME=Gerlach Richard , CITY=Sudbury , COUNTRY=CA , ATYP=Non-US Individual|(US20200114310)|NAME=GERLACH Richard , CITY=Sudbury , COUNTRY=CA|(US20190321777)|NAME=Gerlach Richard , CITY=Sudbury , COUNTRY=CA (US11426695)|NAME=Kramer & Amado, P.C. (US11426695)|CA|(US20200114310)|CA|(US20190321777)|CA (US11426695)|NAME=Gerlach Richard, CITY=Sudbury, COUNTRY=CA|(US20200114310)|NAME=GERLACH Richard, CITY=Sudbury, COUNTRY=CA|(US20190321777)|NAME=Gerlach Richard, CITY=Sudbury, COUNTRY=CA 20 1 Titre: (US11426695)|Media and air filters for carbon dioxide sequestration Résumé: (US11426695)|Filter media and filters for the sequestration of carbon dioxide are disclosed. The carbon dioxide sequestering filter media incorporate silicate minerals, and the carbon dioxide sequestering filters incorporate carbon dioxide sequestering filter media. Filters using only carbon dioxide sequestering media and filters combining carbon dioxide sequestering media with traditional air filter media are disclosed. The carbon dioxide sequestering filters may be used instead of traditional air filters in residential, commercial and industrial applications. 5 Abstract gpt-4o-mini no The article focuses on filter media for CO₂ sequestration, which falls under systems of filtration rather than accelerated weathering or mineral carbonation.
7 CN202111472123 CN202111472123 CN114367179|CN114367179 99681653 CN114367179 B 2023-04-11 [CN114367179B]|CN114367179 A 2022-04-19 [CN114367179] 2021-12-03 2021-12-03 2023-04-11|2022-04-19 (CN114367179B)|2023-04-11 (CN114367179)|2041-12-03 (CN114367179)|Denitration carbon fixing agent using steel slag as raw material and preparation method and application thereof (CN114367179)|The invention relates to the field of flue gas treatment, in particular to a denitration carbon sequestration agent with steel slag as a raw material and a preparation method and application of the denitration carbon sequestration agent. The denitration carbon sequestration agent comprises a reducing agent, an active agent, a complexing agent, a combustion improver, an initiator and a stabilizer, and the stabilizer is a steel slag extract; the method comprises the following steps: respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver; the method comprises the following steps: crushing steel slag, dipping the crushed steel slag in an acid solution for first heating, and then cooling and standing to respectively obtain a supernatant and a lower precipitate; performing evaporation and first roasting on the supernatant liquid to obtain a stabilizer; washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent; the preparation method comprises the following steps: mixing a stabilizer, an active agent, a reducing agent, a complexing agent, an initiator and a combustion improver, and grinding to obtain the dry efficient denitration carbon sequestration agent. According to the application, the denitration carbon sequestration agent is applied to an SNCR denitration process. SHOUGANG GROUP (CN114367179)|SHOUGANG GROUP CO., LTD. ([CN])|(CN114367179)|SHOUGANG GROUP CO., LTD. ([CN]) REN SIDA|ZHAO SHIQI|ZHAO ZHIXING (CN114367179)|REN SIDA|ZHAO SHIQI|ZHAO ZHIXING|(CN114367179)|REN SIDA|ZHAO SHIQI|ZHAO ZHIXING (CN114367179)|GUO SHICHAO;BEIJING BRIGHT & RIGHT LAW FIRM|Reg. Nb: 11302 (CN114367179)|(2) The denitration carbon fixing agent provided by the embodiment of the application has high denitration efficiency, can reach 84% at most, has stable performance, does not produce secondary pollution to the environment, can be widely applied to denitration of flue gas of a high-temperature industrial furnace, and can fix part of CO in the flue gas in a form of generating carbonate in an SNCR reaction temperature interval 2 And carbon emission reduction is realized while denitration is performed.|Compared with the prior art, the technical scheme provided by the embodiment of the application has the following advantages:|The stabilizer has the advantages that the stabilizer can stabilize the denitration carbon fixing agent for denitration and can stabilize the components in the range of 20-40 parts by weight; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is caused that the existence of excessive stabilizer can reduce the denitration efficiency and aggravate the scaling of the hearth; when the value of the weight part is less than the minimum value of the endpoint in the range, the adverse effect is that the content of the stabilizer is too low, so that the components in the denitration carbon fixing agent cannot be stabilized, and the denitration carbon fixing agent cannot be denitrated smoothly.|In the application, the active agent comprises at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide and zirconium oxide, and the positive effect is that the active agent is limited, so that the active agent can promote the denitration carbon-fixing agent to carry out denitration reaction, and meanwhile, as the active agent is common steel slag impurities, corresponding active agent substances can be extracted from the steel slag.|Meanwhile, a steel plant can produce a large amount of steel slag in the smelting process, the large amount of steel slag is often treated as waste, and the existing steel slag has a small recycling range and is often used for producing building materials, so that the steel plant has small profit; therefore, how to apply the steel slag in the flue gas denitration technology is a technical problem which needs to be solved urgently at present.|The positive effect of the initiator of 4-6 parts by weight is that the initiator can fully promote denitration solid carbon to carry out reaction in the range of the parts by weight, thereby ensuring the full proceeding of denitration; when the value of the weight portion is larger than the maximum value of the end point of the range, the adverse effect is that the denitration agent is easy to decompose due to excessive initiator, so that the denitration efficiency is unstable, and the stable storage of the denitration agent is not facilitated; when the value of the weight part is less than the minimum value of the endpoint in the range, the content of the initiator is too low, and the denitration carbon fixing agent cannot be successfully denitrated.| (CN114367179)|1. The denitration carbon fixing agent taking steel slag as a raw material is characterized by comprising the following components in parts by weight: reducing agent: 90-150 parts of an active agent: 1.2-3.3 parts of complexing agent: 1.0-3.0 parts of combustion improver: 0.5-2.0 parts of initiator: 4-6 parts of stabilizer: 20-40 parts of a stabilizer, wherein the stabilizer is a steel slag extract, and the steel slag extract contains CaO and MgO;the active agent comprises at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide and zirconium oxide.| (CN114367179)|In a second aspect, the present application provides a preparation method of a denitration carbon-fixing agent using steel slag as a raw material, the method comprising:|The application provides a denitration carbon-fixing agent taking steel slag as a raw material, and a preparation method and application thereof, which aim to solve the technical problem that the steel slag in the prior art is difficult to apply in a flue gas denitration technology. In a first aspect, the present application provides a denitration carbon fixation agent using steel slag as a raw material, and the denitration carbon fixation agent comprises, by weight: reducing agent: 90-150 parts of an active agent: 1.2-3.3 parts of complexing agent: 1.0-3.0 parts of combustion improver: 0.5-2.0 parts of initiator: 4-6 parts of stabilizer: 20-40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|The application relates to the field of flue gas treatment, in particular to a denitration carbon-fixing agent taking steel slag as a raw material and a preparation method and application thereof; the denitration carbon fixation agent comprises: the steel slag stabilizer comprises a reducing agent, an active agent, a complexing agent, a combustion improver, an initiator and a stabilizer, wherein the stabilizer is a steel slag extract; the method comprises the following steps: respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver; crushing the steel slag, soaking the crushed steel slag in an acid solution for first heating, and then cooling and standing the steel slag to respectively obtain supernatant and lower-layer precipitates; evaporating and first roasting the supernatant to obtain a stabilizer; washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent; mixing a stabilizer, an active agent, a reducing agent, a complexing agent, an initiator and a combustion improver, and then grinding to obtain a dry high-efficiency denitration carbon fixing agent; the application comprises the step of applying the denitration carbon fixing agent to an SNCR denitration process. The application relates to the field of flue gas treatment, in particular to a denitration carbon-fixing agent taking steel slag as a raw material, and a preparation method and application thereof.| (CN114367179)|DENITRATION CARBON FIXING(100,69)|STEEL SLAG(100,51)|RAW MATERIAL(100,21)|COMBUSTION IMPROVER(93,49)|STEEL SLAG EXTRACT(62,14)|STABILIZER(59,47)|HEARTH SCALING(53,1)|CRUSHED STEEL SLAG(51,10)|STABILIZER EXISTENCE(50,1)|STEEL SLAG IMPURITY(50,1)|INITIATOR(49,38)|DENITRATION(48,35)|DENITRATION FULL PROCEEDING(48,1)|STEEL SLAG STABILIZER(48,1)|SLAG IMPURITY(44,1)|DENITRATION CARBON SEQUESTRATION(43,6)|DENITRATION CARBON FIXATION(42,13)|FLUE GAS DENITRATION(37,4)|ROASTING(34,9)|ULTRASONIC OSCILLATION(33,7)|COMPLEXING AGENT(32,45)|SUPERNATANT(30,8)|DENITRATION SOLID CARBON(27,1)|CONTAMINATION(26,1)|FULL PROCEEDING(26,1)|ACTIVE AGENT(24,37)|DENITRATION REACTION(24,7)|TREATING FLUE GAS(24,2)|DENITRATION STABLE STORAGE(24,1)|FLUE GAS(23,10)|POTASSIUM PERMANGANATE(22,8)|STEEL PLANT(18,2)|CARBON FIXATION(17,26)|POLYPROPYLENE ALCOHOL(17,4)|INDUSTRIAL FURNACE(17,1)|SMELTING(17,1)|ACTIVE IRON OXIDE(16,9)|DENITRATION(16,4)|REACTION TEMPERATURE INTERVAL(16,1)|TITANIUM DIOXIDE(15,9)|ZIRCONIUM OXIDE(15,7)|ACTIVE AGENT SUBSTANCE(15,1)|REDUCING AGENT(14,41)|ACIDIC SOLUTION(14,14)|POLYALLYLAMINE(14,2)|ENDPOINT(13,14)|POLYACRYLONITRILE(13,4)|CAO(12,6)|POLYCARBONATE(12,6)|MGO(12,4)|CARBON EMISSION REDUCTION(12,2)|COPPER OXIDE(10,7)|POLLUTANT ULTRALOW EMISSION(10,1)|ACTIVATED CARBON POWDER(9,10)|IRON OXIDE(9,10)|AMMONIUM PERSULFATE(9,7)|AMMONIUM OXALATE(9,6)|POLYAMIDE(9,6)|SODIUM CARBOXYMETHYLCELLULOSE(9,5)|STABLE STORAGE(9,1)|FLY ASH(8,8)|SODIUM BICARBONATE(8,8)|DENITRATION RATE(8,6)|POLYETHYLENE GLYCOL(8,6)|POTASSIUM DIHYDROGEN PHOSPHATE(8,6)|SODIUM PERSULFATE(8,5)|POLYVINYL ALCOHOL(8,4)|ROASTING OXIDATION(8,2)|SUPERNATANT LIQUOR(8,2)|WASTE STEEL SLAG(8,2)|SMALL RECYCLING RANGE(8,1)|AMMONIUM CHLORIDE(7,6)|SODIUM CARBONATE(7,6)|DENITRIFIER DECOMPOSITION(7,1)|POLLUTANT SYNERGISTIC TREATMENT(7,1)|MANGANESE(6,6)|LOW LAYER PRECIPITATE(6,5)|POLYACRYLAMIDE(6,5)|LOWER LAYER PRECIPITATE(6,2)|RESIDUAL IMPURITY(6,2)|SODIUM CARBOXY METHYL CELLULOSE(6,2)|BUILDING MATERIAL PRODUCTION(6,1)|CREATIVE EFFORT SHALL FALL(6,1)|NONEXCLUSIVE INCLUSION(6,1)|WATER BATH HEATING MODE(5,5)|ACTIVATION(5,3)|ENDPOINT VALUE MINIMUM(5,3)|BUILDING MATERIAL(5,1)|CONVERTER STEEL SLAG(5,1)|DENITRATION CARBON FIXATION APPEARANCE(5,1)|DENITRATION CATALYST(5,1)|DENITRATION INJECTION RESISTANCE(5,1)|GERMAN TESTO(5,1)|HUGE CHALLENGE(5,1)|INSUFFICIENT LEACHING(5,1)|ULTRASONIC OSCILLATION TIME(4,9)|CARBON FIXATION RATE(4,6)|STANDING TIME(4,6)|NOX(4,5)|SCR(4,3)|HEARTH(4,2)|STABLE REACTION(4,2)|STABLE STEEL(4,2)|THOUGHT(4,2)|UREA AQUEOUS SOLUTION(4,2)|ACTIVATOR SELECTION(4,1)|AEROSOL GENERATOR(4,1)|AMMONIA ESCAPE(4,1)|DENITRATION SHAPE MAINTENANCE(4,1)|QUANTITATIVE INJECTION(4,1)|RELEVANT LAW(4,1)|SLAG EXTRACT(4,1)|TOO LITTLE COMBUSTION IMPROVER(4,1)|TREATING POLLUTION(4,1)|PARTICLE SIZE(3,5)|ROOM TEMPERATURE(3,4)|ACID SOLUBLE SPECIES(3,1)|CALCINATION(3,1)|DENITRATION DISPERSION DEGREE(3,1)|DENITRATION TEMPERATURE(3,1)|DENITRATION VALUE(3,1)|DENITRIFIER COMPONENT(3,1)|DOUBLE SUBTRACTION(3,1)|FURNACE TEMPERATURE PROMOTION(3,1)|INTEGRAL DENITRATION CARBON FIXING(3,1)|MOISTURE ABSORBING(3,1)|ORDINARY SKILL PERSON(3,1)|PURIFICATION TREATMENT(3,1)|RELATIONAL TERM(3,1)|STABLE DENITRATION CARBON FIXING(3,1)||(CN114367179)|DENITRATION CARBON FIXING(100,70)|STEEL SLAG(100,53)|RAW MATERIAL(100,21)|COMBUSTION IMPROVER(98,49)|STABILIZER(61,47)|DENITRATION(58,37)|HEARTH SCALING(55,1)|CRUSHED STEEL SLAG(53,10)|STEEL SLAG EXTRACT(52,13)|STABILIZER EXISTENCE(52,1)|INITIATOR(51,38)|DENITRATION FULL PROCEEDING(50,1)|STEEL SLAG STABILIZER(50,1)|DENITRATION CARBON SEQUESTRATION(45,6)|FLUE GAS DENITRATION(44,3)|COMPLEXING AGENT(41,44)|DENITRATION CARBON FIXATION(36,12)|ROASTING(36,9)|SUPERNATANT(32,8)|DENITRATION SOLID CARBON(29,1)|FULL PROCEEDING(28,1)|CONTAMINATION(27,1)|POLYACRYLONITRILE(26,4)|TREATING FLUE GAS(25,2)|DENITRATION STABLE STORAGE(25,1)|REACTION TEMPERATURE INTERVAL2AND(25,1)|FLUE GAS(24,10)|APPLICATION PALM(22,4)|POLYCARBONATE(21,6)|INDUSTRIAL FURNACE FLUE GAS(21,1)|STEEL PLANT(19,2)|ACTIVE AGENT(18,37)|CARBON FIXATION(18,26)|SODIUM CARBOXYMETHYLCELLULOSE(18,5)|POLYPROPYLENE ALCOHOL(18,4)|INDUSTRIAL FURNACE(18,1)|SMELTING(18,1)|DENITRATION(17,4)|REDUCING AGENT(15,41)|ACIDIC SOLUTION(15,14)|POLYVINYL ALCOHOL(15,4)|POLYETHYLENE GLYCOL(14,6)|POLYALLYLAMINE(14,3)|ENDPOINT(13,15)|DENITRATION REACTION(13,7)|CARBON EMISSION REDUCTION(13,2)|WATER SOLUBLE COMPLEXING AGENT(13,1)|POTASSIUM PERMANGANATE(12,8)|POLLUTANT ULTRALOW EMISSION(11,1)|STABLE STORAGE(10,1)|ACTIVATED CARBON POWDER(9,10)|TITANIUM DIOXIDE(9,9)|FLY ASH(9,8)|AMMONIUM PERSULFATE(9,7)|AMMONIUM OXALATE(9,6)|DENITRATION RATE(9,6)|POLYAMIDE(9,6)|POTASSIUM DIHYDROGEN PHOSPHATE(9,6)|SODIUM PERSULFATE(9,5)|DENITRATION CATALYST2REACTION(9,1)|SMALL RECYCLING RANGE(9,1)|SODIUM BICARBONATE(8,8)|ZIRCONIUM OXIDE(8,7)|AMMONIUM CHLORIDE(8,6)|SODIUM CARBONATE(8,6)|ROASTING OXIDATION(8,2)|SUPERNATANT LIQUOR(8,2)|DENITRIFIER DECOMPOSITION(8,1)|INITIATOR RULE(8,1)|POLLUTANT SYNERGISTIC TREATMENT(8,1)|ULTRASONIC OSCILLATION TIME(7,9)|LOW LAYER PRECIPITATE(7,5)|RESIDUAL IMPURITY(7,2)|SODIUM CARBOXY METHYL CELLULOSE(7,2)|BUILDING MATERIAL PRODUCTION(7,1)|NONEXCLUSIVE INCLUSION(7,1)|STEEL SLAG IMPURITY(7,1)|MANGANESE(6,6)|POLYACRYLAMIDE(6,4)|BUILDING MATERIAL(6,1)|CONVERTER STEEL SLAG(6,1)|CREATIVE EFFORT(6,1)|DENITRATION CARBON FIXATION APPEARANCE(6,1)|DENITRATION INJECTION RESISTANCE(6,1)|GERMAN TESTO(6,1)|HUGE CHALLENGE(6,1)|INSUFFICIENT LEACHING(6,1)|WASTE STEEL SLAG(6,1)|COPPER OXIDE(5,7)|CAO(5,5)|WATER BATH HEATING MODE(5,5)|ACTIVATION(5,3)|ENDPOINT VALUE MINIMUM(5,3)|LOWER LAYER PRECIPITATE(5,3)|ACTIVATOR SELECTION(5,1)|AEROSOL GENERATOR(5,1)|AMMONIA ESCAPE(5,1)|DENITRATION SHAPE MAINTENANCE(5,1)|QUANTITATIVE INJECTION(5,1)|RELEVANT LAW(5,1)|SLAG EXTRACT(5,1)|TOO LITTLE COMBUSTION IMPROVER(5,1)|TREATING POLLUTION(5,1)|CARBON FIXATION RATE(4,6)|STANDING TIME(4,6)|NOX(4,5)|PARTICLE SIZE(4,5)|STABILIZING AGENT(4,5)|WATER BATH HEATING TEMPERATURE(4,5)|ROOM TEMPERATURE(4,4)|HEARTH(4,2)|INVESTMENT(4,2)|STABLE REACTION(4,2)|STABLE STEEL(4,2)|THOUGHT(4,2)|UREA AQUEOUS SOLUTION(4,2)|ACID SOLUBLE SPECIES(4,1)|BIG DIFFERENCE(4,1)|CALCINATION(4,1)|DENITRATION DISPERSION DEGREE(4,1)|DENITRATION TEMPERATURE(4,1)|DENITRATION VALUE(4,1)|DENITRIFIER COMPONENT(4,1)|DOUBLE SUBTRACTION(4,1)|FURNACE TEMPERATURE PROMOTION(4,1)|INTEGRAL DENITRATION CARBON FIXING(4,1)|MOISTURE ABSORBING(4,1)|PURIFICATION TREATMENT(4,1)|RELATIONAL TERM(4,1)| (CN114367179)|1. The denitration carbon fixing agent taking steel slag as a raw material is characterized by comprising the following components in parts by weight: reducing agent: 90-150 parts of an active agent: 1.2-3.3 parts of complexing agent: 1.0-3.0 parts of combustion improver: 0.5-2.0 parts of initiator: 4-6 parts of stabilizer: 20-40 parts of a stabilizer, wherein the stabilizer is a steel slag extract, and the steel slag extract contains CaO and MgO;|the active agent comprises at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide and zirconium oxide.|2. The denitration carbon sequestration agent of claim 1, wherein the reducing agent comprises at least one of urea, ammonium oxalate, ammonium chloride, polyallylamine, polyamide, sodium bicarbonate and sodium carbonate.|3. The denitration carbon sequestration agent according to claim 1, wherein the complexing agent comprises at least one of sodium carboxymethylcellulose, polyvinyl alcohol, polyethylene glycol, polypropylene alcohol, polyacrylonitrile and polycarbonate.|4. The denitration carbon-fixing agent of claim 1, wherein the initiator comprises at least one of ammonium persulfate, sodium persulfate and potassium dihydrogen phosphate.|5. The denitration carbon sequestration agent as claimed in claim 1, wherein the combustion improver comprises activated carbon powder and/or fly ash.|6. A method for preparing the denitration carbon fixing agent as set forth in any one of claims 1 to 5, wherein the method comprises:|respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver;|crushing the steel slag, soaking the crushed steel slag in an acid solution for first heating, and then cooling and standing the steel slag to respectively obtain supernatant and lower-layer precipitates;|evaporating and first roasting the supernatant to obtain a stabilizer;|washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent;|mixing the stabilizer, the activator, the reducing agent, the complexing agent, the initiator and the combustion improver, and then grinding to obtain a dry high-efficiency denitration carbon fixing agent;|the first heating includes: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the time of ultrasonic oscillation is 6-12 h, and the temperature of water bath heating is 40-100 ℃.|7. The method as claimed in claim 6, wherein the temperature of the first roasting is 600-900 ℃, and the time of the first roasting is 2-8 h;|the temperature of the second roasting is 400-700 ℃, and the time of the second roasting is 3-7 h.|8. The method of claim 6,|the particle size of the crushed steel slag is less than or equal to 200 meshes;|the cooling comprises the following steps: naturally cooling to room temperature;|the standing time is 6-24 h.|9. An application of the denitration carbon-fixing agent using steel slag as a raw material, which is characterized by comprising the step of using the denitration carbon-fixing agent as defined in any one of claims 1 to 5 in an SNCR denitration process. (CN114367179)|TECHNICAL FIELD|[0001] The application relates to the field of flue gas treatment, in particular to a denitration carbon-fixing agent taking steel slag as a raw material, and a preparation method and application thereof.|BACKGROUND ART|[0002] With further improvement and enhancement of the relevant laws and regulations for preventing and controlling the atmospheric pollution in China, the emission limit standard of pollutants is lower and lower, the emission of industrial sources is the most main atmospheric pollution source, and the purification treatment of industrial flue gas faces huge challenges aiming at the requirement of ultralow emission of pollutants such as nitrogen oxides and the like.|[0003] The current commonly used flue gas denitration technology is divided into two types, one type is selective catalytic reduction technology (SCR), the other type is selective non-catalytic reduction technology (SNCR), the two maximum differences are whether to use a catalyst, the SCR technology can be widely applied due to the existence of the catalyst to reach higher denitration efficiency (more than 90%) at lower flue gas temperature, but the SCR technology has the defects of higher one-time investment, additional reactor construction and easy poisoning and abrasion of the catalyst; the SNCR technology directly sprays a denitrifier into a hearth, reduces nitrogen oxide (NOx) into nitrogen and water at high temperature, does not need to additionally establish a reactor like SCR, has low investment, but has low denitration efficiency which is only 30-50 percent and does not accord with the current emission standard, and at the same time, most of the SNCR technologies usually adopt ammonia water or urea aqueous solution as the denitrifier, can reduce the temperature in the furnace after being sprayed into the hearth, and is not beneficial to the denitration reaction in the SNCR.|[0004] Meanwhile, a steel plant can produce a large amount of steel slag in the smelting process, the large amount of steel slag is often treated as waste, and the existing steel slag has a small recycling range and is often used for producing building materials, so that the steel plant has small profit; therefore, how to apply the steel slag in the flue gas denitration technology is a technical problem which needs to be solved urgently at present.|DISCLOSURE|Disclosure of Invention|[0005] The application provides a denitration carbon-fixing agent taking steel slag as a raw material, and a preparation method and application thereof, which aim to solve the technical problem that the steel slag in the prior art is difficult to apply in a flue gas denitration technology.|[0006] In a first aspect, the present application provides a denitration carbon fixation agent using steel slag as a raw material, and the denitration carbon fixation agent comprises, by weight: reducing agent: 90-150 parts of an active agent: 1.2-3.3 parts of complexing agent: 1.0-3.0 parts of combustion improver: 0.5-2.0 parts of initiator: 4-6 parts of stabilizer: 20-40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0007] Optionally, the active agent includes at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide, and zirconium oxide.|[0008] Optionally, the reducing agent comprises at least one of urea, ammonium oxalate, ammonium chloride, polyallylamine, polyamide, sodium bicarbonate and sodium carbonate.|[0009] Optionally, the complexing agent includes at least one of sodium carboxymethylcellulose, polyvinyl alcohol, polyethylene glycol, polypropylene alcohol, polyacrylonitrile, and polycarbonate.|[0010] Optionally, the initiator comprises at least one of ammonium persulfate, sodium persulfate, and potassium dihydrogen phosphate.|[0011] Optionally, the combustion improver comprises activated carbon powder and/or fly ash.|[0012] In a second aspect, the present application provides a preparation method of a denitration carbon-fixing agent using steel slag as a raw material, the method comprising:|[0013] respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver;|[0014] crushing the steel slag, soaking the crushed steel slag in an acid solution for first heating, and then cooling and standing to respectively obtain a supernatant and a lower precipitate;|[0015] evaporating and first roasting the supernatant to obtain a stabilizer;|[0016] washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent;|[0017] and mixing the stabilizer, the activator, the reducing agent, the complexing agent, the initiator and the combustion improver, and then grinding to obtain the dry efficient denitration carbon fixing agent.|[0018] Optionally, the first roasting temperature is 600-900 ℃, and the first roasting time is 2-8 h;|[0019] the temperature of the second roasting is 400-700 ℃, and the time of the second roasting is 3-7 h.|[0020] Optionally, the first heating comprises: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the ultrasonic oscillation time is 6-12 h, and the water bath heating temperature is 40-100 ℃;|[0021] the particle size of the crushed steel slag is less than or equal to 200 meshes;|[0022] the cooling comprises the following steps: naturally cooling to room temperature;|[0023] the standing time is 6-24 h.|[0024] In a third aspect, the application provides an application of the denitration carbon-fixing agent using steel slag as a raw material, and the application comprises the step of using the denitration carbon-fixing agent in the SNCR denitration process.|[0025] Compared with the prior art, the technical scheme provided by the embodiment of the application has the following advantages:|[0026] according to the denitration carbon fixing agent taking the steel slag as the raw material, the steel slag extract is used as the stabilizer, and then the reducing agent, the activating agent, the complexing agent, the combustion improver and the initiator are sequentially matched, so that the stable denitration carbon fixing agent is formed, the waste steel slag and the SNCR technology are combined together, and a new thought and a formula are provided for preparing the SNCR denitration agent.|DRAWINGS DESCRIPTION|[0027] The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the invention and together with the description, serve to explain the principles of the invention.|[0028] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.|[0029] Fig. 1 is a schematic flow chart of a method provided in an embodiment of the present application;|[0030] FIG. 2 is a diagram illustrating the activity evaluation of a denitration carbon sequestration agent provided by an embodiment of the present application;|[0031] fig. 3 is an appearance diagram of the denitration carbon sequestration agent provided by the embodiment of the application.|INVENTION MODE|Detailed Description|[0032] In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are some embodiments of the present application, but not all embodiments. All other embodiments obtained by a person of ordinary skill in the art based on the embodiments in the present application without making creative efforts shall fall within the protection scope of the present application.|[0033] The inventive idea of the application is as follows: because the waste steel slag contains oxides of iron, manganese, calcium, magnesium and the like, particularly the converter steel slag contains 40 to 50 percent of CaO and 6 to 10 percent of MgO, the CaO not only can be used as a drying agent to prevent the denitration agent from deliquescing, but also can react with CO within an SNCR reaction temperature window (800 to 1000 ℃) to form a denitration catalyst 2 Reaction to form CaCO 3 Thereby realizing partial CO while denitrating 2 Trapping to achieve the purpose of treating pollution by waste and controlling NOx and CO 2 The purpose of "double subtraction".|[0034] In one embodiment of the present invention, a denitration carbon fixation agent using steel slag as a raw material is provided, which includes, by weight: reducing agent: 90-150 parts of an active agent: 1.2-3.3 parts of complexing agent: 1.0-3.0 parts of combustion improver: 0.5-2.0 parts of initiator: 4-6 parts of stabilizer: 20-40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0035] In the application, the positive effects that the reducing agent accounts for 90-150 parts by weight are that nitrogen oxides in the steelmaking stage can be reduced into nitrogen and water in the weight fraction range, and meanwhile, a stabilizer and an activator can be matched to realize denitration and carbon fixation; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is that the content of the reducing agent is too much, the denitration agent is easy to absorb moisture and harden, so that the power consumption of a fan is increased, even pipelines are blocked when the power consumption is serious, and the excessive reducing agent not only increases the preparation cost, but also easily causes the escape of ammonia; when the value of the weight part is less than the endpoint minimum value in the range, the adverse effect is that the content of the reducing agent is too low, the denitration efficiency of the denitration agent is reduced, and the operation cost is increased.|[0036] The positive effect of the activator with the weight portion of 1.2-3.3 portions is that the denitration carbon fixing agent can be fully activated within the weight portion range, so that nitrogen oxide in the steelmaking stage is reduced into nitrogen and water, and simultaneously, the denitration carbon fixing agent can be matched with the stabilizer to realize denitration carbon fixing; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is that the content of the active agent is too much, the reducing agent is decomposed too fast, the reducing gas cannot be in full contact with NOx, the denitration efficiency is reduced, meanwhile, the active agent has certain hygroscopicity, and the injection resistance of the denitration agent is increased due to the excessive active agent; when the value of weight portion is less than the endpoint minimum value in this range, the adverse effect that will lead to is that the active agent content is too low, will cause the denitrifier to decompose inadequately to influence denitration efficiency, thereby perhaps need to improve furnace temperature in order to accelerate the decomposition of denitrifier, but furnace temperature's promotion can make a small amount of ammonia turn into NOx, thereby reduces denitration efficiency.|[0037] The positive effect of the complexing agent with the weight portion of 1.0-3.0 portions is that the denitration carbon fixation agent can be fixed together in the weight portion range, thereby promoting the denitration carbon fixation and reducing the nitrogen oxide in the steelmaking stage into nitrogen and water by the denitration carbon fixation agent; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is that the content of the complexing agent is too much, and the denitration agent is easy to agglomerate and appear at high temperature, so that the dispersion degree of the denitration agent during injection is reduced, the denitration efficiency is influenced, and a pipeline can be blocked when the denitration efficiency is serious; when the value of the weight part is less than the endpoint minimum value in the range, the adverse effect is that the content of the complexing agent is too low, so that the components of the denitrifier cannot be effectively complexed together, thereby affecting the denitration efficiency.|[0038] The positive effect of the combustion improver of 0.5 to 2.0 parts by weight is that the combustion improver can burn in the range of the parts by weight, thereby maintaining the temperature of the denitration fixed stage and leading the denitration carbon fixing agent to be capable of reacting stably; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is that excessive combustion improver cannot ensure that the denitration carbon fixing agent is carried out at a proper reaction temperature, so that the denitration carbon fixing agent cannot be fully denitrated, and when the value of the weight part is smaller than the minimum value of the end point of the range, the adverse effect is that too little combustion improver cannot ensure that the denitration carbon fixing agent can reach an effective denitration temperature, and the reducing agent cannot effectively work.|[0039] The positive effect of the initiator of 4-6 parts by weight is that the initiator can fully promote denitration solid carbon to carry out reaction in the range of the parts by weight, thereby ensuring the full proceeding of denitration; when the value of the weight portion is larger than the maximum value of the end point of the range, the adverse effect is that the denitration agent is easy to decompose due to excessive initiator, so that the denitration efficiency is unstable, and the stable storage of the denitration agent is not facilitated; when the value of the weight part is less than the minimum value of the endpoint in the range, the content of the initiator is too low, and the denitration carbon fixing agent cannot be successfully denitrated.|[0040] The stabilizer has the advantages that the stabilizer can stabilize the denitration carbon fixing agent for denitration and can stabilize the components in the range of 20-40 parts by weight; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is caused that the existence of excessive stabilizer can reduce the denitration efficiency and aggravate the scaling of the hearth; when the value of the weight part is less than the minimum value of the endpoint in the range, the adverse effect is that the content of the stabilizer is too low, so that the components in the denitration carbon fixing agent cannot be stabilized, and the denitration carbon fixing agent cannot be denitrated smoothly.|[0041] In some embodiments, the active agent comprises at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide, and zirconium oxide, and the active agent comprises an extract of steel slag.|[0042] In the application, the active agent comprises at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide and zirconium oxide, and the positive effect is that the active agent is limited, so that the active agent can promote the denitration carbon-fixing agent to carry out denitration reaction, and meanwhile, as the active agent is common steel slag impurities, corresponding active agent substances can be extracted from the steel slag.|[0043] In some embodiments, the reducing agent comprises at least one of urea, ammonium oxalate, ammonium chloride, polyacrylamide, polyamide, sodium bicarbonate, and sodium carbonate.|[0044] In the application, the positive effect that the reducing agent comprises at least one of urea, ammonium oxalate, ammonium chloride, polyacrylamide, sodium bicarbonate and sodium carbonate is that the cost of the integral denitration carbon fixing agent is reduced by selecting the conventional reducing agent.|[0045] In some embodiments, the complexing agent comprises at least one of sodium carboxymethylcellulose, polyvinyl alcohol, polyethylene glycol, polyacrylonitrile, and polycarbonate.|[0046] In the application, the complexing agent comprises at least one of sodium carboxymethylcellulose, polyvinyl alcohol, polyethylene glycol, polyacrylonitrile and polycarbonate, and the positive effect is that the complexing agent is limited to be a common water-soluble complexing agent, so that the overall cost of the denitration carbon fixing agent can be fully reduced.|[0047] In some embodiments, the initiator comprises at least one of ammonium persulfate, sodium persulfate, and potassium dihydrogen phosphate.|[0048] In the application, the positive effect that the initiator comprises at least one of ammonium persulfate, sodium persulfate and potassium dihydrogen phosphate is that the overall cost of the denitration carbon fixing agent can be reduced by limiting the source of the initiator.|[0049] In some embodiments, the combustion improver comprises activated carbon powder and/or fly ash.|[0050] In the application, the combustion improver comprises the activated carbon powder and/or the fly ash, and the positive effects are that the overall cost of the denitration carbon fixing agent can be further reduced by limiting the conventional combustion improver, and the reaction temperature and the carbon content of the denitration carbon fixing agent can be further ensured.|[0051] In an embodiment of the present application, as shown in fig. 1, a method for preparing a denitration carbon-fixing agent using steel slag as a raw material is provided, the method including:|[0052] s1, respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver;|[0053] s2, crushing the steel slag, soaking the crushed steel slag in an acid solution for first heating, cooling and standing to obtain a supernatant and a lower precipitate respectively;|[0054] s3, evaporating and roasting the supernatant liquor to obtain a stabilizer;|[0055] s4, washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent;|[0056] and S5, mixing the stabilizer, the activator, the reducer, the complexing agent, the initiator and the combustion improver, and then grinding to obtain the dry efficient denitration carbon fixing agent, wherein the acidic solution can be acetic acid.|[0057] In some embodiments, the temperature of the first roasting is 600 ℃ to 900 ℃, and the time of the first roasting is 2h to 8h;|[0058] the temperature of the second roasting is 400-700 ℃, and the time of the second roasting is 3-7 h.|[0059] In the application, the positive effect that the first roasting temperature is 600-900 ℃ is that in the temperature range, the proper roasting temperature can fully sinter elements leached by acid solution in the steel slag and form a stable steel slag extract, so that a proper amount of CaO and MgO can be provided, nitrogen oxides and carbon dioxide in the denitration reaction are stabilized, and the stable reaction of the denitration carbon fixing agent is realized; when the value of the temperature is larger than the maximum value of the endpoint of the range, the adverse effect is that the excessive temperature can cause Ca and Mg in the steel slag to be converted into other substances, and the stable proceeding of the denitration reaction of the denitration carbon fixing agent is influenced.|[0060] The positive effect that the first roasting time is 2-8 h is that in the time range, elements leached out by acid solution in the steel slag can be fully sintered and form a stable steel slag extract, so that a proper amount of CaO and MgO can be provided, nitrogen oxides and carbon dioxide in the denitration reaction are stabilized, and the stable reaction of the denitration carbon fixing agent is realized; when the value of the time is larger than the maximum value of the end point of the range, the adverse effect is that the too long roasting time not only increases the process time consumption, but also causes the excessive oxidation of oxides such as iron, manganese, calcium, magnesium and the like in the steel slag to influence the performance of the stabilizer, thereby influencing the performance of the obtained denitration carbon fixing agent.|[0061] The positive effect of the second roasting temperature of 400-700 ℃ is that in the temperature range, iron element, manganese element, copper element, carbon element or zirconium element in the residual impurities which cannot be leached by the acid solution can be fully sintered into corresponding substances of active iron oxide, potassium permanganate, copper oxide, titanium dioxide or zirconium oxide, so that a stable activating agent is formed, the denitration carbon fixing agent can be fully activated, and the denitration reaction is promoted to be carried out; when the value of the temperature is greater than the maximum value of the end point of the range, the adverse effect is that the too high temperature causes the roasting oxidation of the iron element, the manganese element, the copper element, the carbon element or the zirconium element to be excessive, so that the effect of the activator is affected, and the denitration effect of the denitration carbon fixing agent is reduced.|[0062] The second roasting time is 3-7 h, and the positive effect is that in the time range, iron element, manganese element, copper element, carbon element or zirconium element in the residual impurities which cannot be leached by the acid solution can be fully sintered into corresponding substances of active iron oxide, potassium permanganate, copper oxide, titanium dioxide or zirconium oxide, so that a stable activating agent is formed, the denitration carbon fixing agent can be fully activated, and the denitration reaction is promoted to be carried out; when the value of the time is larger than the maximum value of the end point of the range, the time consumption of the process is increased due to overlong time, and meanwhile, the roasting oxidation of the iron element, the manganese element, the copper element, the carbon element or the zirconium element is excessive due to overlong time, so that the effect of the activator is influenced, and the denitration effect of the denitration carbon fixing agent is reduced.|[0063] In some embodiments, the first heating comprises: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the ultrasonic oscillation time is 6-12 h, and the water bath heating temperature is 40-100 ℃;|[0064] the particle size of the crushed steel slag is less than or equal to 200 meshes;|[0065] the cooling comprises the following steps: naturally cooling to room temperature;|[0066] the standing time is 6-24 h.|[0067] In the application, the positive effect that the ultrasonic oscillation time is 6-12 h is that substances which are soluble in an acid solution in the steel slag can be fully dissolved in the solution within the time range, so that the mutual influence between the prepared stabilizing agent and an activating agent is avoided, the function of the denitration carbon-fixing agent is limited, and meanwhile, substances which are soluble in acid and substances which are difficult to dissolve in acid can be fully separated out within a proper time; when the time value is greater than the maximum value of the end point of the range, the time consumption of the process is increased due to too long time, and when the time value is less than the minimum value of the end point of the range, the time is too short, substances which are soluble in an acidic solution and substances which are difficult to dissolve in the acidic solution in the steel slag cannot be sufficiently dissolved and separated, so that the functions of a subsequent activating agent and a stabilizing agent are interfered with each other, and the denitration and carbon fixation effects of the denitration carbon fixation agent are influenced.|[0068] The crushed steel slag has the positive effect that the grain size is less than or equal to 200 meshes, and in the grain size range, the steel slag can be fully leached out of substances which can be dissolved in acid through the first heating of an acid solution, and can be beneficial to the second roasting to form an activating agent; when the particle size is greater than the end maximum of this range, this can have the adverse effect that too large a particle size will result in insufficient leaching of the acid soluble species, while the second calcination will not form a suitable activator.|[0069] In one embodiment of the application, the application of the denitration carbon-fixing agent using the steel slag as the raw material comprises the step of using the denitration carbon-fixing agent in an SNCR denitration process.|[0070] Example 1|[0071] A denitration carbon fixing agent using steel slag as a raw material comprises the following components in parts by weight: reducing agent: 90 parts, active agent: 2 parts, complexing agent: 1.0 part, combustion improver: 0.6 part, initiator: 4 parts and a stabilizer: 20 parts of the stabilizing agent is steel slag extract, and the stabilizing agent contains a large amount of CaO and can be directly replaced by CaO.|[0072] The activator comprises active ferric oxide and potassium permanganate which are mixed according to the mass ratio of 1: 1.|[0073] The reducing agent is ammonium chloride.|[0074] The complexing agent is sodium carboxymethyl cellulose.|[0075] The initiator is ammonium persulfate.|[0076] The combustion improver is fly ash.|[0077] As shown in fig. 1, a preparation method of a denitration carbon-fixing agent using steel slag as a raw material comprises the following steps:|[0078] s1, respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver;|[0079] s2, crushing the steel slag, soaking the crushed steel slag in an acid solution for first heating, cooling and standing to obtain a supernatant and a lower precipitate respectively;|[0080] s3, evaporating and roasting the supernatant liquor to obtain a stabilizer;|[0081] s4, washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent;|[0082] and S5, mixing the stabilizer, the activator, the reducer, the complexing agent, the initiator and the combustion improver, and then grinding to obtain the dry efficient denitration carbon fixing agent.|[0083] The temperature of the first roasting is 600 ℃, and the time of the first roasting is 4 hours;|[0084] the temperature of the second roasting is 550 ℃, and the time of the second roasting is 6h.|[0085] The first heating includes: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the time of ultrasonic oscillation is 6h, and the temperature of water bath heating is 60 ℃;|[0086] the grain size of the crushed steel slag is less than or equal to 200 meshes;|[0087] the cooling comprises the following steps: naturally cooling to room temperature;|[0088] the standing time is 12h.|[0089] Example 2|[0090] Comparing example 2 with example 1, example 2 differs from example 1 in that:|[0091] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 100 parts, active agent: 2 parts, complexing agent: 1.2 parts of a combustion improver: 1 part, initiator: 6 parts and a stabilizer: 35 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0092] The active agent is active ferric oxide.|[0093] The reducing agent is urea, sodium bicarbonate and sodium carbonate with the mass ratio of 3: 1.|[0094] The complexing agent is polyethylene glycol.|[0095] The initiator is potassium dihydrogen phosphate.|[0096] The combustion improver is activated carbon powder.|[0097] Example 3|[0098] Comparing example 3 with example 1, example 3 differs from example 1 in that:|[0099] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 140 parts, active agent: 2.0 parts, complexing agent: 2 parts of a combustion improver: 2.0 parts, initiator: 5 parts and a stabilizer: 30 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0100] The activator is a mixture of active iron oxide and copper oxide with the mass ratio of 3: 1.|[0101] The reducing agent is a mixture of urea, ammonium oxalate, sodium bicarbonate and sodium carbonate with the mass ratio of 24: 2: 1.|[0102] The complexing agent is polypropylene alcohol.|[0103] The initiator is sodium persulfate.|[0104] The combustion improver is a mixture of activated carbon powder and fly ash with the mass ratio of 1: 1.|[0105] Example 4|[0106] Comparing example 4 with example 1, example 4 differs from example 1 in that:|[0107] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 110 parts, active agent: 2 parts of complexing agent: 2.6 parts of a combustion improver: 1.0 part, initiator: 4 parts and a stabilizer: 25 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0108] The active agents are active ferric oxide and titanium dioxide with the mass ratio of 1: 1.|[0109] The reducing agent is a mixture of urea, polyacrylamide and sodium bicarbonate with the mass ratio of 20: 1.|[0110] The complexing agent is polycarbonate.|[0111] The initiator is potassium persulfate.|[0112] The combustion improver is activated carbon powder.|[0113] Example 5|[0114] Comparing example 5 with example 1, example 5 differs from example 1 in that:|[0115] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 150 parts, active agent: 3 parts of complexing agent: 2 parts of a combustion improver: 1 part, initiator: 4 parts and a stabilizer: 40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0116] The active agent is a mixture of active iron oxide, titanium dioxide and zirconium oxide with the mass ratio of 3: 2: 1.|[0117] The reducing agent is a mixture of urea, polyacrylamide and polyamide in a mass ratio of 28: 1.|[0118] The complexing agent is sodium carboxymethyl cellulose.|[0119] The initiator is ammonium persulfate.|[0120] The combustion improver is activated carbon powder and fly ash with the ratio of 2: 1.|[0121] Example 6|[0122] Comparing example 6 with example 1, example 6 differs from example 1 in that:|[0123] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 130 parts, active agent: 1.2 parts, complexing agent: 3 parts of a combustion improver: 0.5 part, initiator: 4 parts and a stabilizer: 40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0124] The active agent is a mixture of active iron oxide and titanium dioxide with the mass ratio of 1: 1.|[0125] The reducing agent is a mixture of urea, ammonium chloride and polyamide in a mass ratio of 23: 6: 1.|[0126] The complexing agent is sodium carboxymethylcellulose and polyethylene glycol in a ratio of 1: 1.|[0127] The initiator is potassium dihydrogen phosphate.|[0128] The combustion improver is activated carbon powder and fly ash with the ratio of 1: 2.|[0129] Example 7|[0130] Comparing example 7 with example 1, example 7 differs from example 1 in that:|[0131] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 140 parts, active agent: 3.3 parts, complexing agent: 3 parts of a combustion improver: 0.5 part, initiator: 4 parts and a stabilizer: 40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0132] The active agent is potassium permanganate.|[0133] The reducing agent is a mixture of urea, ammonium oxalate, sodium bicarbonate, polyacrylamide and polyamide in a mass ratio of 20: 4: 1.|[0134] The complexing agent is 1: 1 polypropylene alcohol and polycarbonate.|[0135] The initiator is ammonium persulfate.|[0136] The combustion improver is activated carbon powder.|[0137] Example 8|[0138] Comparing example 8 with example 1, example 6 differs from example 1 in that:|[0139] the temperature of the first roasting is 650 ℃, and the time of the first roasting is 2 hours;|[0140] the temperature of the second roasting is 400 ℃, and the time of the second roasting is 3h.|[0141] The ultrasonic oscillation time is 7h, and the water bath heating temperature is 40 ℃;|[0142] the standing time is 6h.|[0143] Example 9|[0144] Comparing example 9 with example 1, example 7 differs from example 1 in that:|[0145] the temperature of the first roasting is 900 ℃, and the time of the first roasting is 8 hours;|[0146] the temperature of the second roasting is 700 ℃, and the time of the second roasting is 7h.|[0147] The first heating includes: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the ultrasonic oscillation time is 12h, and the water bath heating temperature is 100 ℃;|[0148] the standing time is 24h.|[0149] Comparative example 1|[0150] Comparative example 1 and example 1 were compared, and comparative example 1 and example 1 were distinguished in that:|[0151] no stabilizer was added.|[0152] Comparative example 2|[0153] Comparative example 2 is compared with example 1, and comparative example 2 differs from example 1 in that:|[0154] no activator was added.|[0155] Comparative example 3|[0156] Comparative example 3 is compared with example 1, and comparative example 3 differs from example 1 in that:|[0157] the temperature of the first roasting is 550 ℃, and the time of the first roasting is 1h;|[0158] the temperature of the second roasting is 350 ℃, and the time of the second roasting is 2h.|[0159] The ultrasonic oscillation time is 5h, and the water bath heating temperature is 35 ℃.|[0160] Comparative example 4|[0161] Comparative example 4 is compared with example 1, and comparative example 4 differs from example 1 in that:|[0162] the temperature of the first roasting is 1000 ℃, and the time of the first roasting is 10 hours;|[0163] the temperature of the second roasting is 800 ℃, and the time of the second roasting is 8h.|[0164] The ultrasonic oscillation time is 14h, and the oil bath heating temperature is 110 ℃.|[0165] Related experiments:|[0166] the denitration carbon fixation agents obtained in examples 1 to 7 and comparative examples 1 to 4 were collected, and performance tests were performed on each denitration carbon fixation agent, and the results are shown in table 1.|[0167] Test methods of the related experiments:|[0168] denitration rate: and (3) carrying out activity evaluation on the high-efficiency denitration carbon-fixing agent by adopting a self-made reactor, wherein the concentration of nitrogen oxide is controlled to be 450ppm, carrying out quantitative injection on the high-efficiency denitration carbon-fixing agent by using a German Topas SAG-420 type dust aerosol generator, detecting the concentration of NOx at the inlet and the outlet of the reactor by using a German testo 350 flue gas analyzer, and calculating the denitration rate.|[0169] Carbon fixation rate: and testing by adopting a testing method and equipment with the same denitration rate.|[0170] TABLE 1 denitration and carbon fixation Activity of examples and comparative examples|[0171] |[0172] |[0173] Table 1 specific analysis:|[0174] the denitration rate refers to the efficiency of the denitration carbon-fixing agent in actual use, wherein the denitration rate indicates that the denitration carbon-fixing agent has higher and more stable activity when being higher.|[0175] The carbon fixation rate refers to the efficiency of the denitration carbon fixation agent in the use of the reagent, which can absorb carbon dioxide, and the higher the carbon fixation rate is, the better the removal effect of the denitration carbon fixation agent on carbon dioxide is.|[0176] From the data for examples 1-7 it can be seen that:|[0177] the denitration efficiency of the denitration carbon fixing agent provided by the invention mainly depends on the weight of the reducing agent, but the denitration efficiency is slowly increased after the weight of the reducing agent reaches a certain fraction, which indicates that the optimum range of the weight of the reducing agent exists.|[0178] The selection of the activator has obvious influence on the denitration activity, and the proper activator can enhance the denitration activity under the condition of the same weight part of the reducing agent.|[0179] Although the complexing agent, the combustion improver and the initiator have little influence on the value of the denitration efficiency, the complexing agent, the combustion improver and the initiator have obvious influence on the dispersibility and the shape maintenance of the denitration agent in use.|[0180] The carbon fixation rate is mainly influenced by the content of the stabilizer, the larger the specific gravity of the stabilizer in parts by weight is, the more the carbon fixation amount is, the influence of the reaction temperature is avoided, the integral carbon fixation rate is not good, but the carbon fixation rate still has certain beneficial values on the synergistic treatment of multiple pollutants and carbon emission reduction.|[0181] From the data of comparative examples 1-4, it can be seen that:|[0182] the stabilizer not only can influence the carbon fixation rate, but also has certain influence on the stability of the appearance of the denitration carbon fixation agent provided by the application.|[0183] The activator has a remarkable influence on the denitration efficiency, so that if the roasting temperature is low, the crystal form of the activator is influenced, the activity of the activator is reduced, and the denitration efficiency is influenced; if the roasting temperature is too high, agglomeration and increase of active agent particles are caused, and the denitration efficiency is also influenced. Therefore, the selection of the appropriate weight fraction of the stabilizer and the activator and the preparation method have a significant influence on the denitration rate and the carbon fixation amount of the denitration carbon fixation agent provided by the invention.|[0184] One or more technical solutions in the embodiments of the present application at least have the following technical effects or advantages:|[0185] (1) The denitration carbon fixing agent provided by the embodiment of the application obtains the extract by processing the steel slag, the extract of the steel slag is used as the stabilizing agent, and the formed denitration carbon fixing agent can effectively remove nitrogen oxides and fix carbon dioxide, so that a new thought is provided for the denitration agent.|[0186] (2) The denitration carbon fixing agent provided by the embodiment of the application has high denitration efficiency, can reach 84% at most, has stable performance, does not produce secondary pollution to the environment, can be widely applied to denitration of flue gas of a high-temperature industrial furnace, and can fix part of CO in the flue gas in a form of generating carbonate in an SNCR reaction temperature interval 2 And carbon emission reduction is realized while denitration is performed.|[0187] (3) The denitration carbon fixing agent provided by the embodiment of the application is stable in performance and convenient to transport because the denitration carbon fixing agent is solid powder, and can not reduce the temperature in the furnace like ammonia water and urea aqueous solution when being used, thereby reducing the operation and maintenance cost.|[0188] (4) According to the method provided by the embodiment of the application, due to the adoption of two-stage roasting treatment, substances in the steel slag can be fully extracted and respectively used as an active agent and a stabilizing agent, so that the use application of the steel slag is expanded, and the method can be used in the steel-making industry to realize the circular economy effect.|[0189] The drawings illustrate:|[0190] fig. 2 is an activity evaluation diagram of the denitration carbon sequestration agent provided in the embodiment of the present application, and as can be seen from fig. 2, the denitration activity tends to increase first and then decrease with the increase of the reaction temperature, and the denitration activity reaches the highest activity at 900 ℃, and the optimal reaction temperature region is 800 ℃ to 1000 ℃.|[0191] Fig. 3 is an appearance diagram of the denitration carbon fixing agent provided in the embodiment of the present application, and as can be seen from fig. 3, the denitration carbon fixing agent obtained in the present application is light yellow, and has uniform particle distribution, stable performance and convenient transportation.|[0192] It is noted that, in this document, relational terms such as "first" and "second," and the like, are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrases "comprising a," "8230," "8230," or "comprising" does not exclude the presence of additional like elements in a process, method, article, or apparatus that comprises the element.|[0193] The above description is merely illustrative of particular embodiments of the invention that enable those skilled in the art to understand or practice the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. (CN114367179)|TECHNICAL FIELD|[0001] The application relates to the field of flue gas treatment, in particular to a denitration carbon-fixing agent taking steel slag as a raw material, and a preparation method and application thereof.|BACKGROUND ART|[0002] With further improvement and enhancement of the relevant laws and regulations for preventing and controlling the atmospheric pollution in China, the emission limit standard of pollutants is lower and lower, the emission of industrial sources is the most main atmospheric pollution source, and the purification treatment of industrial flue gas faces huge challenges aiming at the requirement of ultralow emission of pollutants such as nitrogen oxides and the like.|[0003] The current commonly used flue gas denitration technology is divided into two types, one type is selective catalytic reduction technology (SCR), the other type is selective non-catalytic reduction technology (SNCR), the two maximum differences are whether to use a catalyst, the SCR technology can be widely applied due to the existence of the catalyst to reach higher denitration efficiency (more than 90%) at lower flue gas temperature, but the SCR technology has the defects of higher one-time investment, additional reactor construction and easy poisoning and abrasion of the catalyst; the SNCR technology directly sprays a denitrifier into a hearth, reduces nitrogen oxide (NOx) into nitrogen and water at high temperature, does not need to additionally establish a reactor like SCR, has low investment, but has low denitration efficiency which is only 30-50 percent and does not accord with the current emission standard, and at the same time, most of the SNCR technologies usually adopt ammonia water or urea aqueous solution as the denitrifier, can reduce the temperature in the furnace after being sprayed into the hearth, and is not beneficial to the denitration reaction in the SNCR.|[0004] Meanwhile, a steel plant can produce a large amount of steel slag in the smelting process, the large amount of steel slag is often treated as waste, and the existing steel slag has a small recycling range and is often used for producing building materials, so that the steel plant has small profit; therefore, how to apply the steel slag in the flue gas denitration technology is a technical problem which needs to be solved urgently at present.|DISCLOSURE|Disclosure of Invention|[0005] The application provides a denitration carbon-fixing agent taking steel slag as a raw material, and a preparation method and application thereof, which aim to solve the technical problem that the steel slag in the prior art is difficult to apply in a flue gas denitration technology.|[0006] In a first aspect, the present application provides a denitration carbon fixation agent using steel slag as a raw material, and the denitration carbon fixation agent comprises, by weight: reducing agent: 90-150 parts of an active agent: 1.2-3.3 parts of complexing agent: 1.0-3.0 parts of combustion improver: 0.5-2.0 parts of initiator: 4-6 parts of stabilizer: 20-40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0007] Optionally, the active agent includes at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide, and zirconium oxide.|[0008] Optionally, the reducing agent comprises at least one of urea, ammonium oxalate, ammonium chloride, polyallylamine, polyamide, sodium bicarbonate and sodium carbonate.|[0009] Optionally, the complexing agent includes at least one of sodium carboxymethylcellulose, polyvinyl alcohol, polyethylene glycol, polypropylene alcohol, polyacrylonitrile, and polycarbonate.|[0010] Optionally, the initiator comprises at least one of ammonium persulfate, sodium persulfate, and potassium dihydrogen phosphate.|[0011] Optionally, the combustion improver comprises activated carbon powder and/or fly ash.|[0012] In a second aspect, the present application provides a preparation method of a denitration carbon-fixing agent using steel slag as a raw material, the method comprising:|[0013] respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver;|[0014] crushing the steel slag, soaking the crushed steel slag in an acid solution for first heating, and then cooling and standing to respectively obtain a supernatant and a lower precipitate;|[0015] evaporating and first roasting the supernatant to obtain a stabilizer;|[0016] washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent;|[0017] and mixing the stabilizer, the activator, the reducing agent, the complexing agent, the initiator and the combustion improver, and then grinding to obtain the dry efficient denitration carbon fixing agent.|[0018] Optionally, the first roasting temperature is 600-900 ℃, and the first roasting time is 2-8 h;|[0019] the temperature of the second roasting is 400-700 ℃, and the time of the second roasting is 3-7 h.|[0020] Optionally, the first heating comprises: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the ultrasonic oscillation time is 6-12 h, and the water bath heating temperature is 40-100 ℃;|[0021] the particle size of the crushed steel slag is less than or equal to 200 meshes;|[0022] the cooling comprises the following steps: naturally cooling to room temperature;|[0023] the standing time is 6-24 h.|[0024] In a third aspect, the application provides an application of the denitration carbon-fixing agent using steel slag as a raw material, and the application comprises the step of using the denitration carbon-fixing agent in the SNCR denitration process.|[0025] Compared with the prior art, the technical scheme provided by the embodiment of the application has the following advantages:|[0026] according to the denitration carbon fixing agent taking the steel slag as the raw material, the steel slag extract is used as the stabilizer, and then the reducing agent, the activating agent, the complexing agent, the combustion improver and the initiator are sequentially matched, so that the stable denitration carbon fixing agent is formed, the waste steel slag and the SNCR technology are combined together, and a new thought and a formula are provided for preparing the SNCR denitration agent.|DRAWINGS DESCRIPTION|[0027] The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the invention and together with the description, serve to explain the principles of the invention.|[0028] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.|[0029] Fig. 1 is a schematic flow chart of a method provided in an embodiment of the present application;|[0030] FIG. 2 is a diagram illustrating the activity evaluation of a denitration carbon sequestration agent provided by an embodiment of the present application;|[0031] fig. 3 is an appearance diagram of the denitration carbon sequestration agent provided by the embodiment of the application.|INVENTION MODE|Detailed Description|[0032] In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are some embodiments of the present application, but not all embodiments. All other embodiments obtained by a person of ordinary skill in the art based on the embodiments in the present application without making creative efforts shall fall within the protection scope of the present application.|[0033] The inventive idea of the application is as follows: because the waste steel slag contains oxides of iron, manganese, calcium, magnesium and the like, particularly the converter steel slag contains 40 to 50 percent of CaO and 6 to 10 percent of MgO, the CaO not only can be used as a drying agent to prevent the denitration agent from deliquescing, but also can react with CO within an SNCR reaction temperature window (800 to 1000 ℃) to form a denitration catalyst 2 Reaction to form CaCO 3 Thereby realizing partial CO while denitrating 2 Trapping to achieve the purpose of treating pollution by waste and controlling NOx and CO 2 The purpose of "double subtraction".|[0034] In one embodiment of the present invention, a denitration carbon fixation agent using steel slag as a raw material is provided, which includes, by weight: reducing agent: 90-150 parts of an active agent: 1.2-3.3 parts of complexing agent: 1.0-3.0 parts of combustion improver: 0.5-2.0 parts of initiator: 4-6 parts of stabilizer: 20-40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0035] In the application, the positive effects that the reducing agent accounts for 90-150 parts by weight are that nitrogen oxides in the steelmaking stage can be reduced into nitrogen and water in the weight fraction range, and meanwhile, a stabilizer and an activator can be matched to realize denitration and carbon fixation; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is that the content of the reducing agent is too much, the denitration agent is easy to absorb moisture and harden, so that the power consumption of a fan is increased, even pipelines are blocked when the power consumption is serious, and the excessive reducing agent not only increases the preparation cost, but also easily causes the escape of ammonia; when the value of the weight part is less than the endpoint minimum value in the range, the adverse effect is that the content of the reducing agent is too low, the denitration efficiency of the denitration agent is reduced, and the operation cost is increased.|[0036] The positive effect of the activator with the weight portion of 1.2-3.3 portions is that the denitration carbon fixing agent can be fully activated within the weight portion range, so that nitrogen oxide in the steelmaking stage is reduced into nitrogen and water, and simultaneously, the denitration carbon fixing agent can be matched with the stabilizer to realize denitration carbon fixing; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is that the content of the active agent is too much, the reducing agent is decomposed too fast, the reducing gas cannot be in full contact with NOx, the denitration efficiency is reduced, meanwhile, the active agent has certain hygroscopicity, and the injection resistance of the denitration agent is increased due to the excessive active agent; when the value of weight portion is less than the endpoint minimum value in this range, the adverse effect that will lead to is that the active agent content is too low, will cause the denitrifier to decompose inadequately to influence denitration efficiency, thereby perhaps need to improve furnace temperature in order to accelerate the decomposition of denitrifier, but furnace temperature's promotion can make a small amount of ammonia turn into NOx, thereby reduces denitration efficiency.|[0037] The positive effect of the complexing agent with the weight portion of 1.0-3.0 portions is that the denitration carbon fixation agent can be fixed together in the weight portion range, thereby promoting the denitration carbon fixation and reducing the nitrogen oxide in the steelmaking stage into nitrogen and water by the denitration carbon fixation agent; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is that the content of the complexing agent is too much, and the denitration agent is easy to agglomerate and appear at high temperature, so that the dispersion degree of the denitration agent during injection is reduced, the denitration efficiency is influenced, and a pipeline can be blocked when the denitration efficiency is serious; when the value of the weight part is less than the endpoint minimum value in the range, the adverse effect is that the content of the complexing agent is too low, so that the components of the denitrifier cannot be effectively complexed together, thereby affecting the denitration efficiency.|[0038] The positive effect of the combustion improver of 0.5 to 2.0 parts by weight is that the combustion improver can burn in the range of the parts by weight, thereby maintaining the temperature of the denitration fixed stage and leading the denitration carbon fixing agent to be capable of reacting stably; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is that excessive combustion improver cannot ensure that the denitration carbon fixing agent is carried out at a proper reaction temperature, so that the denitration carbon fixing agent cannot be fully denitrated, and when the value of the weight part is smaller than the minimum value of the end point of the range, the adverse effect is that too little combustion improver cannot ensure that the denitration carbon fixing agent can reach an effective denitration temperature, and the reducing agent cannot effectively work.|[0039] The positive effect of the initiator of 4-6 parts by weight is that the initiator can fully promote denitration solid carbon to carry out reaction in the range of the parts by weight, thereby ensuring the full proceeding of denitration; when the value of the weight portion is larger than the maximum value of the end point of the range, the adverse effect is that the denitration agent is easy to decompose due to excessive initiator, so that the denitration efficiency is unstable, and the stable storage of the denitration agent is not facilitated; when the value of the weight part is less than the minimum value of the endpoint in the range, the content of the initiator is too low, and the denitration carbon fixing agent cannot be successfully denitrated.|[0040] The stabilizer has the advantages that the stabilizer can stabilize the denitration carbon fixing agent for denitration and can stabilize the components in the range of 20-40 parts by weight; when the value of the weight part is larger than the maximum value of the end point of the range, the adverse effect is caused that the existence of excessive stabilizer can reduce the denitration efficiency and aggravate the scaling of the hearth; when the value of the weight part is less than the minimum value of the endpoint in the range, the adverse effect is that the content of the stabilizer is too low, so that the components in the denitration carbon fixing agent cannot be stabilized, and the denitration carbon fixing agent cannot be denitrated smoothly.|[0041] In some embodiments, the active agent comprises at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide, and zirconium oxide, and the active agent comprises an extract of steel slag.|[0042] In the application, the active agent comprises at least one of active iron oxide, potassium permanganate, copper oxide, titanium dioxide and zirconium oxide, and the positive effect is that the active agent is limited, so that the active agent can promote the denitration carbon-fixing agent to carry out denitration reaction, and meanwhile, as the active agent is common steel slag impurities, corresponding active agent substances can be extracted from the steel slag.|[0043] In some embodiments, the reducing agent comprises at least one of urea, ammonium oxalate, ammonium chloride, polyacrylamide, polyamide, sodium bicarbonate, and sodium carbonate.|[0044] In the application, the positive effect that the reducing agent comprises at least one of urea, ammonium oxalate, ammonium chloride, polyacrylamide, sodium bicarbonate and sodium carbonate is that the cost of the integral denitration carbon fixing agent is reduced by selecting the conventional reducing agent.|[0045] In some embodiments, the complexing agent comprises at least one of sodium carboxymethylcellulose, polyvinyl alcohol, polyethylene glycol, polyacrylonitrile, and polycarbonate.|[0046] In the application, the complexing agent comprises at least one of sodium carboxymethylcellulose, polyvinyl alcohol, polyethylene glycol, polyacrylonitrile and polycarbonate, and the positive effect is that the complexing agent is limited to be a common water-soluble complexing agent, so that the overall cost of the denitration carbon fixing agent can be fully reduced.|[0047] In some embodiments, the initiator comprises at least one of ammonium persulfate, sodium persulfate, and potassium dihydrogen phosphate.|[0048] In the application, the positive effect that the initiator comprises at least one of ammonium persulfate, sodium persulfate and potassium dihydrogen phosphate is that the overall cost of the denitration carbon fixing agent can be reduced by limiting the source of the initiator.|[0049] In some embodiments, the combustion improver comprises activated carbon powder and/or fly ash.|[0050] In the application, the combustion improver comprises the activated carbon powder and/or the fly ash, and the positive effects are that the overall cost of the denitration carbon fixing agent can be further reduced by limiting the conventional combustion improver, and the reaction temperature and the carbon content of the denitration carbon fixing agent can be further ensured.|[0051] In an embodiment of the present application, as shown in fig. 1, a method for preparing a denitration carbon-fixing agent using steel slag as a raw material is provided, the method including:|[0052] s1, respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver;|[0053] s2, crushing the steel slag, soaking the crushed steel slag in an acid solution for first heating, cooling and standing to obtain a supernatant and a lower precipitate respectively;|[0054] s3, evaporating and roasting the supernatant liquor to obtain a stabilizer;|[0055] s4, washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent;|[0056] and S5, mixing the stabilizer, the activator, the reducer, the complexing agent, the initiator and the combustion improver, and then grinding to obtain the dry efficient denitration carbon fixing agent, wherein the acidic solution can be acetic acid.|[0057] In some embodiments, the temperature of the first roasting is 600 ℃ to 900 ℃, and the time of the first roasting is 2h to 8h;|[0058] the temperature of the second roasting is 400-700 ℃, and the time of the second roasting is 3-7 h.|[0059] In the application, the positive effect that the first roasting temperature is 600-900 ℃ is that in the temperature range, the proper roasting temperature can fully sinter elements leached by acid solution in the steel slag and form a stable steel slag extract, so that a proper amount of CaO and MgO can be provided, nitrogen oxides and carbon dioxide in the denitration reaction are stabilized, and the stable reaction of the denitration carbon fixing agent is realized; when the value of the temperature is larger than the maximum value of the endpoint of the range, the adverse effect is that the excessive temperature can cause Ca and Mg in the steel slag to be converted into other substances, and the stable proceeding of the denitration reaction of the denitration carbon fixing agent is influenced.|[0060] The positive effect that the first roasting time is 2-8 h is that in the time range, elements leached out by acid solution in the steel slag can be fully sintered and form a stable steel slag extract, so that a proper amount of CaO and MgO can be provided, nitrogen oxides and carbon dioxide in the denitration reaction are stabilized, and the stable reaction of the denitration carbon fixing agent is realized; when the value of the time is larger than the maximum value of the end point of the range, the adverse effect is that the too long roasting time not only increases the process time consumption, but also causes the excessive oxidation of oxides such as iron, manganese, calcium, magnesium and the like in the steel slag to influence the performance of the stabilizer, thereby influencing the performance of the obtained denitration carbon fixing agent.|[0061] The positive effect of the second roasting temperature of 400-700 ℃ is that in the temperature range, iron element, manganese element, copper element, carbon element or zirconium element in the residual impurities which cannot be leached by the acid solution can be fully sintered into corresponding substances of active iron oxide, potassium permanganate, copper oxide, titanium dioxide or zirconium oxide, so that a stable activating agent is formed, the denitration carbon fixing agent can be fully activated, and the denitration reaction is promoted to be carried out; when the value of the temperature is greater than the maximum value of the end point of the range, the adverse effect is that the too high temperature causes the roasting oxidation of the iron element, the manganese element, the copper element, the carbon element or the zirconium element to be excessive, so that the effect of the activator is affected, and the denitration effect of the denitration carbon fixing agent is reduced.|[0062] The second roasting time is 3-7 h, and the positive effect is that in the time range, iron element, manganese element, copper element, carbon element or zirconium element in the residual impurities which cannot be leached by the acid solution can be fully sintered into corresponding substances of active iron oxide, potassium permanganate, copper oxide, titanium dioxide or zirconium oxide, so that a stable activating agent is formed, the denitration carbon fixing agent can be fully activated, and the denitration reaction is promoted to be carried out; when the value of the time is larger than the maximum value of the end point of the range, the time consumption of the process is increased due to overlong time, and meanwhile, the roasting oxidation of the iron element, the manganese element, the copper element, the carbon element or the zirconium element is excessive due to overlong time, so that the effect of the activator is influenced, and the denitration effect of the denitration carbon fixing agent is reduced.|[0063] In some embodiments, the first heating comprises: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the ultrasonic oscillation time is 6-12 h, and the water bath heating temperature is 40-100 ℃;|[0064] the particle size of the crushed steel slag is less than or equal to 200 meshes;|[0065] the cooling comprises the following steps: naturally cooling to room temperature;|[0066] the standing time is 6-24 h.|[0067] In the application, the positive effect that the ultrasonic oscillation time is 6-12 h is that substances which are soluble in an acid solution in the steel slag can be fully dissolved in the solution within the time range, so that the mutual influence between the prepared stabilizing agent and an activating agent is avoided, the function of the denitration carbon-fixing agent is limited, and meanwhile, substances which are soluble in acid and substances which are difficult to dissolve in acid can be fully separated out within a proper time; when the time value is greater than the maximum value of the end point of the range, the time consumption of the process is increased due to too long time, and when the time value is less than the minimum value of the end point of the range, the time is too short, substances which are soluble in an acidic solution and substances which are difficult to dissolve in the acidic solution in the steel slag cannot be sufficiently dissolved and separated, so that the functions of a subsequent activating agent and a stabilizing agent are interfered with each other, and the denitration and carbon fixation effects of the denitration carbon fixation agent are influenced.|[0068] The crushed steel slag has the positive effect that the grain size is less than or equal to 200 meshes, and in the grain size range, the steel slag can be fully leached out of substances which can be dissolved in acid through the first heating of an acid solution, and can be beneficial to the second roasting to form an activating agent; when the particle size is greater than the end maximum of this range, this can have the adverse effect that too large a particle size will result in insufficient leaching of the acid soluble species, while the second calcination will not form a suitable activator.|[0069] In one embodiment of the application, the application of the denitration carbon-fixing agent using the steel slag as the raw material comprises the step of using the denitration carbon-fixing agent in an SNCR denitration process.|[0070] Example 1|[0071] A denitration carbon fixing agent using steel slag as a raw material comprises the following components in parts by weight: reducing agent: 90 parts, active agent: 2 parts, complexing agent: 1.0 part, combustion improver: 0.6 part, initiator: 4 parts and a stabilizer: 20 parts of the stabilizing agent is steel slag extract, and the stabilizing agent contains a large amount of CaO and can be directly replaced by CaO.|[0072] The activator comprises active ferric oxide and potassium permanganate which are mixed according to the mass ratio of 1: 1.|[0073] The reducing agent is ammonium chloride.|[0074] The complexing agent is sodium carboxymethyl cellulose.|[0075] The initiator is ammonium persulfate.|[0076] The combustion improver is fly ash.|[0077] As shown in fig. 1, a preparation method of a denitration carbon-fixing agent using steel slag as a raw material comprises the following steps:|[0078] s1, respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver;|[0079] s2, crushing the steel slag, soaking the crushed steel slag in an acid solution for first heating, cooling and standing to obtain a supernatant and a lower precipitate respectively;|[0080] s3, evaporating and roasting the supernatant liquor to obtain a stabilizer;|[0081] s4, washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent;|[0082] and S5, mixing the stabilizer, the activator, the reducer, the complexing agent, the initiator and the combustion improver, and then grinding to obtain the dry efficient denitration carbon fixing agent.|[0083] The temperature of the first roasting is 600 ℃, and the time of the first roasting is 4 hours;|[0084] the temperature of the second roasting is 550 ℃, and the time of the second roasting is 6h.|[0085] The first heating includes: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the time of ultrasonic oscillation is 6h, and the temperature of water bath heating is 60 ℃;|[0086] the grain size of the crushed steel slag is less than or equal to 200 meshes;|[0087] the cooling comprises the following steps: naturally cooling to room temperature;|[0088] the standing time is 12h.|[0089] Example 2|[0090] Comparing example 2 with example 1, example 2 differs from example 1 in that:|[0091] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 100 parts, active agent: 2 parts, complexing agent: 1.2 parts of a combustion improver: 1 part, initiator: 6 parts and a stabilizer: 35 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0092] The active agent is active ferric oxide.|[0093] The reducing agent is urea, sodium bicarbonate and sodium carbonate with the mass ratio of 3: 1.|[0094] The complexing agent is polyethylene glycol.|[0095] The initiator is potassium dihydrogen phosphate.|[0096] The combustion improver is activated carbon powder.|[0097] Example 3|[0098] Comparing example 3 with example 1, example 3 differs from example 1 in that:|[0099] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 140 parts, active agent: 2.0 parts, complexing agent: 2 parts of a combustion improver: 2.0 parts, initiator: 5 parts and a stabilizer: 30 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0100] The activator is a mixture of active iron oxide and copper oxide with the mass ratio of 3: 1.|[0101] The reducing agent is a mixture of urea, ammonium oxalate, sodium bicarbonate and sodium carbonate with the mass ratio of 24: 2: 1.|[0102] The complexing agent is polypropylene alcohol.|[0103] The initiator is sodium persulfate.|[0104] The combustion improver is a mixture of activated carbon powder and fly ash with the mass ratio of 1: 1.|[0105] Example 4|[0106] Comparing example 4 with example 1, example 4 differs from example 1 in that:|[0107] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 110 parts, active agent: 2 parts of complexing agent: 2.6 parts of a combustion improver: 1.0 part, initiator: 4 parts and a stabilizer: 25 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0108] The active agents are active ferric oxide and titanium dioxide with the mass ratio of 1: 1.|[0109] The reducing agent is a mixture of urea, polyacrylamide and sodium bicarbonate with the mass ratio of 20: 1.|[0110] The complexing agent is polycarbonate.|[0111] The initiator is potassium persulfate.|[0112] The combustion improver is activated carbon powder.|[0113] Example 5|[0114] Comparing example 5 with example 1, example 5 differs from example 1 in that:|[0115] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 150 parts, active agent: 3 parts of complexing agent: 2 parts of a combustion improver: 1 part, initiator: 4 parts and a stabilizer: 40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0116] The active agent is a mixture of active iron oxide, titanium dioxide and zirconium oxide with the mass ratio of 3: 2: 1.|[0117] The reducing agent is a mixture of urea, polyacrylamide and polyamide in a mass ratio of 28: 1.|[0118] The complexing agent is sodium carboxymethyl cellulose.|[0119] The initiator is ammonium persulfate.|[0120] The combustion improver is activated carbon powder and fly ash with the ratio of 2: 1.|[0121] Example 6|[0122] Comparing example 6 with example 1, example 6 differs from example 1 in that:|[0123] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 130 parts, active agent: 1.2 parts, complexing agent: 3 parts of a combustion improver: 0.5 part, initiator: 4 parts and a stabilizer: 40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0124] The active agent is a mixture of active iron oxide and titanium dioxide with the mass ratio of 1: 1.|[0125] The reducing agent is a mixture of urea, ammonium chloride and polyamide in a mass ratio of 23: 6: 1.|[0126] The complexing agent is sodium carboxymethylcellulose and polyethylene glycol in a ratio of 1: 1.|[0127] The initiator is potassium dihydrogen phosphate.|[0128] The combustion improver is activated carbon powder and fly ash with the ratio of 1: 2.|[0129] Example 7|[0130] Comparing example 7 with example 1, example 7 differs from example 1 in that:|[0131] a denitration carbon fixing agent taking steel slag as a raw material comprises the following components in parts by weight: reducing agent: 140 parts, active agent: 3.3 parts, complexing agent: 3 parts of a combustion improver: 0.5 part, initiator: 4 parts and a stabilizer: 40 parts of a stabilizer, wherein the stabilizer is a steel slag extract.|[0132] The active agent is potassium permanganate.|[0133] The reducing agent is a mixture of urea, ammonium oxalate, sodium bicarbonate, polyacrylamide and polyamide in a mass ratio of 20: 4: 1.|[0134] The complexing agent is 1: 1 polypropylene alcohol and polycarbonate.|[0135] The initiator is ammonium persulfate.|[0136] The combustion improver is activated carbon powder.|[0137] Example 8|[0138] Comparing example 8 with example 1, example 6 differs from example 1 in that:|[0139] the temperature of the first roasting is 650 ℃, and the time of the first roasting is 2 hours;|[0140] the temperature of the second roasting is 400 ℃, and the time of the second roasting is 3h.|[0141] The ultrasonic oscillation time is 7h, and the water bath heating temperature is 40 ℃;|[0142] the standing time is 6h.|[0143] Example 9|[0144] Comparing example 9 with example 1, example 7 differs from example 1 in that:|[0145] the temperature of the first roasting is 900 ℃, and the time of the first roasting is 8 hours;|[0146] the temperature of the second roasting is 700 ℃, and the time of the second roasting is 7h.|[0147] The first heating includes: under the condition of ultrasonic oscillation, carrying out first heating in a water bath heating mode, wherein the ultrasonic oscillation time is 12h, and the water bath heating temperature is 100 ℃;|[0148] the standing time is 24h.|[0149] Comparative example 1|[0150] Comparative example 1 and example 1 were compared, and comparative example 1 and example 1 were distinguished in that:|[0151] no stabilizer was added.|[0152] Comparative example 2|[0153] Comparative example 2 is compared with example 1, and comparative example 2 differs from example 1 in that:|[0154] no activator was added.|[0155] Comparative example 3|[0156] Comparative example 3 is compared with example 1, and comparative example 3 differs from example 1 in that:|[0157] the temperature of the first roasting is 550 ℃, and the time of the first roasting is 1h;|[0158] the temperature of the second roasting is 350 ℃, and the time of the second roasting is 2h.|[0159] The ultrasonic oscillation time is 5h, and the water bath heating temperature is 35 ℃.|[0160] Comparative example 4|[0161] Comparative example 4 is compared with example 1, and comparative example 4 differs from example 1 in that:|[0162] the temperature of the first roasting is 1000 ℃, and the time of the first roasting is 10 hours;|[0163] the temperature of the second roasting is 800 ℃, and the time of the second roasting is 8h.|[0164] The ultrasonic oscillation time is 14h, and the oil bath heating temperature is 110 ℃.|[0165] Related experiments:|[0166] the denitration carbon fixation agents obtained in examples 1 to 7 and comparative examples 1 to 4 were collected, and performance tests were performed on each denitration carbon fixation agent, and the results are shown in table 1.|[0167] Test methods of the related experiments:|[0168] denitration rate: and (3) carrying out activity evaluation on the high-efficiency denitration carbon-fixing agent by adopting a self-made reactor, wherein the concentration of nitrogen oxide is controlled to be 450ppm, carrying out quantitative injection on the high-efficiency denitration carbon-fixing agent by using a German Topas SAG-420 type dust aerosol generator, detecting the concentration of NOx at the inlet and the outlet of the reactor by using a German testo 350 flue gas analyzer, and calculating the denitration rate.|[0169] Carbon fixation rate: and testing by adopting a testing method and equipment with the same denitration rate.|[0170] TABLE 1 denitration and carbon fixation Activity of examples and comparative examples|[0171] |[0172] |[0173] Table 1 specific analysis:|[0174] the denitration rate refers to the efficiency of the denitration carbon-fixing agent in actual use, wherein the denitration rate indicates that the denitration carbon-fixing agent has higher and more stable activity when being higher.|[0175] The carbon fixation rate refers to the efficiency of the denitration carbon fixation agent in the use of the reagent, which can absorb carbon dioxide, and the higher the carbon fixation rate is, the better the removal effect of the denitration carbon fixation agent on carbon dioxide is.|[0176] From the data for examples 1-7 it can be seen that:|[0177] the denitration efficiency of the denitration carbon fixing agent provided by the invention mainly depends on the weight of the reducing agent, but the denitration efficiency is slowly increased after the weight of the reducing agent reaches a certain fraction, which indicates that the optimum range of the weight of the reducing agent exists.|[0178] The selection of the activator has obvious influence on the denitration activity, and the proper activator can enhance the denitration activity under the condition of the same weight part of the reducing agent.|[0179] Although the complexing agent, the combustion improver and the initiator have little influence on the value of the denitration efficiency, the complexing agent, the combustion improver and the initiator have obvious influence on the dispersibility and the shape maintenance of the denitration agent in use.|[0180] The carbon fixation rate is mainly influenced by the content of the stabilizer, the larger the specific gravity of the stabilizer in parts by weight is, the more the carbon fixation amount is, the influence of the reaction temperature is avoided, the integral carbon fixation rate is not good, but the carbon fixation rate still has certain beneficial values on the synergistic treatment of multiple pollutants and carbon emission reduction.|[0181] From the data of comparative examples 1-4, it can be seen that:|[0182] the stabilizer not only can influence the carbon fixation rate, but also has certain influence on the stability of the appearance of the denitration carbon fixation agent provided by the application.|[0183] The activator has a remarkable influence on the denitration efficiency, so that if the roasting temperature is low, the crystal form of the activator is influenced, the activity of the activator is reduced, and the denitration efficiency is influenced; if the roasting temperature is too high, agglomeration and increase of active agent particles are caused, and the denitration efficiency is also influenced. Therefore, the selection of the appropriate weight fraction of the stabilizer and the activator and the preparation method have a significant influence on the denitration rate and the carbon fixation amount of the denitration carbon fixation agent provided by the invention.|[0184] One or more technical solutions in the embodiments of the present application at least have the following technical effects or advantages:|[0185] (1) The denitration carbon fixing agent provided by the embodiment of the application obtains the extract by processing the steel slag, the extract of the steel slag is used as the stabilizing agent, and the formed denitration carbon fixing agent can effectively remove nitrogen oxides and fix carbon dioxide, so that a new thought is provided for the denitration agent.|[0186] (2) The denitration carbon fixing agent provided by the embodiment of the application has high denitration efficiency, can reach 84% at most, has stable performance, does not produce secondary pollution to the environment, can be widely applied to denitration of flue gas of a high-temperature industrial furnace, and can fix part of CO in the flue gas in a form of generating carbonate in an SNCR reaction temperature interval 2 And carbon emission reduction is realized while denitration is performed.|[0187] (3) The denitration carbon fixing agent provided by the embodiment of the application is stable in performance and convenient to transport because the denitration carbon fixing agent is solid powder, and can not reduce the temperature in the furnace like ammonia water and urea aqueous solution when being used, thereby reducing the operation and maintenance cost.|[0188] (4) According to the method provided by the embodiment of the application, due to the adoption of two-stage roasting treatment, substances in the steel slag can be fully extracted and respectively used as an active agent and a stabilizing agent, so that the use application of the steel slag is expanded, and the method can be used in the steel-making industry to realize the circular economy effect.|[0189] The drawings illustrate:|[0190] fig. 2 is an activity evaluation diagram of the denitration carbon sequestration agent provided in the embodiment of the present application, and as can be seen from fig. 2, the denitration activity tends to increase first and then decrease with the increase of the reaction temperature, and the denitration activity reaches the highest activity at 900 ℃, and the optimal reaction temperature region is 800 ℃ to 1000 ℃.|[0191] Fig. 3 is an appearance diagram of the denitration carbon fixing agent provided in the embodiment of the present application, and as can be seen from fig. 3, the denitration carbon fixing agent obtained in the present application is light yellow, and has uniform particle distribution, stable performance and convenient transportation.|[0192] It is noted that, in this document, relational terms such as "first" and "second," and the like, are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrases "comprising a," "8230," "8230," or "comprising" does not exclude the presence of additional like elements in a process, method, article, or apparatus that comprises the element.|[0193] The above description is merely illustrative of particular embodiments of the invention that enable those skilled in the art to understand or practice the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. Family Number|(99681653)|99681653|Abstract|(CN114367179B B)|The invention relates to the field of flue gas treatment , in particular to a denitration carbon sequestration agent with steel slag as a raw material and a preparation method and application of the denitration carbon sequestration agent . The denitration carbon sequestration agent comprises a reducing agent , an active agent , a complexing agent , a combustion improver , an initiator and a stabilizer , and the stabilizer is a steel slag extract ; the method comprises the following steps : respectively obtaining steel slag , a reducing agent , a complexing agent , an initiator and a combustion improver ; the method comprises the following steps : crushing steel slag , dipping the crushed steel slag in an acid solution for first heating , and then cooling and standing to respectively obtain a supernatant and a lower precipitate ; performing evaporation and first roasting on the supernatant liquid to obtain a stabilizer ; washing , filtering and drying the lower - layer precipitate , and then carrying out second roasting to obtain an active agent ; the preparation method comprises the following steps : mixing a stabilizer , an active agent , a reducing agent , a complexing agent , an initiator and a combustion improver , and grinding to obtain the dry efficient denitration carbon sequestration agent . According to the application , the denitration carbon sequestration agent is applied to an SNCR denitration process . |CPC codes|(CN114367179B B)|B01D - 001/00 |B01D - 001/30 |B01D - 053/56 |B01D - 053/62 |B01D - 2251/2067 |B01D - 2251/206 |B01D - 2251/304 |B01D - 2251/602 |B01D - 2251/606 |B01D - 2251/60 |B01D - 2251/80 |B01D - 2258/0283 |IPC codes|(CN114367179B B)|B01D - 001/00 |B01D - 001/30 |B01D - 053/56 |B01D - 053/62 |Title|(CN114367179 A)|Denitration carbon sequestration agent taking steel slag as raw material as well as preparation method and application of denitration carbon sequestration agent | Chemical engineering|Environmental technology B01D-001/00|B01D-001/30|B01D-053/56|B01D-053/62|B01D-2251/206|B01D-2251/2067|B01D-2251/304|B01D-2251/60|B01D-2251/602|B01D-2251/606|B01D-2251/80|B01D-2258/0283|B09B-003/00 B01D-001/00|B01D-001/30|B01D-053/56|B01D-053/62|B01D-2251/206|B01D-2251/2067|B01D-2251/304|B01D-2251/60|B01D-2251/602|B01D-2251/606|B01D-2251/80|B01D-2258/0283|B09B-003/00 B01D-001/00|B01D-001/30|B01D-053/56|B01D-053/62|B09B-003/00|B09B-003/30|B09B-003/35|B09B-003/40|B09B-003/80 B01D-001/00|B01D-001/30|B01D-053/56|B01D-053/62|B09B-003/00|B09B-003/30|B09B-003/35|B09B-003/40|B09B-003/80 CN109777958|CN108246095|CN106861431|US20160177209|CN103801192|CN101851071|US20100068109|US4620492|US20200230551|FR3008326|US20060029535|DE2108059 CN109777958 84551612 WHO=Examiner SELF=N CAT=A|CN108246095 80494932 WHO=Examiner SELF=N CAT=A|CN106861431 76531361 WHO=Examiner SELF=N CAT=A|US20160177209 73362371 WHO=Examiner SELF=N CAT=A|CN103801192 66049065 WHO=Examiner SELF=N CAT=A|CN101851071 7094502 WHO=Examiner SELF=Y CAT=A|US20100068109 6607323 WHO=Examiner SELF=N CAT=A|US4620492 52025222 WHO=Examiner SELF=N CAT=A|US20200230551 78833499 WHO=Examiner SELF=N|FR3008326 68407864 WHO=Examiner SELF=N|US20060029535 43579883 WHO=Examiner SELF=N|DE2108059 12322678 WHO=Examiner SELF=N MENG 等: &quot;Simultaneous removal of SO2 and NOx from flue gas using (NH4)2S2O3/steel slag slurry combined with ozone oxidation&quot;, 《FUEL》 (Cat. A)|王晨晔: &quot;钢渣多金属分离与伴生资源梯级利用&quot;, 《第七届尾矿与冶金渣综合利用技术研讨会暨招远市循环经济项目招商对接会论文集》 (Cat. A) US4620492; US20100068109; CN101851071; CN103801192; US20160177209; CN106861431; CN108246095; CN109777958; FR3008326; US20060029535; US20200230551; DE2108059 GRANTED (CN114367179)|GRANTED ALIVE (CN114367179)|ALIVE (CN114367179)|LEGAL DETAILS FOR CN114367179|Actual or expected expiration date=2041-12-03|Legal state=ALIVE|Status=GRANTED|Event publication date=2021-12-03|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202111472123|Application date=2021-12-03|Standardized application number=2021CN-1472123|Event publication date=2022-04-19|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114367179|Publication stage code=A|Publication date=2022-04-19|Standardized publication number=CN114367179|Event publication date=2022-04-19|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-05-06|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-04-11|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN114367179|Publication stage code=B|Publication date=2023-04-11|Standardized publication number=CN114367179B|Event publication date=2023-04-11|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN114367179)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTzfvtZ4l5R7xj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067303020&ekey=2319&xpn=CN114367179B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=cm%252FK6qWF43fN46mpcKI9dLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN114367179)|CN|(CN114367179)|CN (CN114367179)|NAME=SHOUGANG GROUP CO., LTD. , COUNTRY=CN|(CN114367179)|NAME=SHOUGANG GROUP CO., LTD. , COUNTRY=CN (CN114367179)|NAME=GUO SHICHAO;BEIJING BRIGHT & RIGHT LAW FIRM , REG=11302|(CN114367179)|NAME=GUO SHICHAO;BEIJING BRIGHT & RIGHT LAW FIRM , REG=11302 (CN114367179)|NAME=REN SIDA|NAME=ZHAO SHIQI|NAME=ZHAO ZHIXING|(CN114367179)|NAME=REN SIDA|NAME=ZHAO SHIQI|NAME=ZHAO ZHIXING 0 1 Titre: (CN114367179)|Denitration carbon fixing agent using steel slag as raw material and preparation method and application thereof Résumé: (CN114367179)|The invention relates to the field of flue gas treatment, in particular to a denitration carbon sequestration agent with steel slag as a raw material and a preparation method and application of the denitration carbon sequestration agent. The denitration carbon sequestration agent comprises a reducing agent, an active agent, a complexing agent, a combustion improver, an initiator and a stabilizer, and the stabilizer is a steel slag extract; the method comprises the following steps: respectively obtaining steel slag, a reducing agent, a complexing agent, an initiator and a combustion improver; the method comprises the following steps: crushing steel slag, dipping the crushed steel slag in an acid solution for first heating, and then cooling and standing to respectively obtain a supernatant and a lower precipitate; performing evaporation and first roasting on the supernatant liquid to obtain a stabilizer; washing, filtering and drying the lower-layer precipitate, and then carrying out second roasting to obtain an active agent; the preparation method comprises the following steps: mixing a stabilizer, an active agent, a reducing agent, a complexing agent, an initiator and a combustion improver, and grinding to obtain the dry efficient denitration carbon sequestration agent. According to the application, the denitration carbon sequestration agent is applied to an SNCR denitration process. 0 Abstract gpt-4o-mini no The article focuses on a denitration carbon sequestration agent using steel slag, which is related to flue gas treatment rather than the accelerated weathering of minerals for CO₂ capture.
8 GB202319995 WOGB2024/051780|GB202319995 GB2636853|WO2025/133560|GB202319995 108540136 WO2025/133560 A1 2025-06-26 [WO2025133560]|GB2636853 A 2025-07-02 [GB2636853]|GB202319995 D0 2024-02-07 [GB202319995] 2023-12-22 2024-07-08|2023-12-22 2025-07-02|2025-06-26|2024-02-07 (WO2025/133560)|2027-06-22|(GB2636853)|2043-12-22 (WO2025/133560)|Enhanced weathering carbon dioxide removal quantification method and apparatus (WO2025/133560)|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. UNDO CARBON (WO2025/133560)|UNDO CARBON LTD ([GB])|(GB2636853)|Undo Carbon Ltd|(GB202319995)|Undo Carbon Ltd LIU XINRAN (WO2025/133560)|LIU, Xinran (WO2025/133560)|BARNES IP LIMITED ([GB]) (WO2025/133560)|However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data.|Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water.| (WO2025/133560)|1. A method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).| (WO2025/133560)|According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water.|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water.| (WO2025/133560)|SOIL SAMPLE(100,77)|CARBON DIOXIDE(100,18)|ENHANCED WEATHERING(100,11)|PORE WATER SAMPLE(100,5)|ENHANCED WEATHERING CARBON DIOXIDE(100,2)|REMOVAL QUANTIFICATION(100,2)|ENHANCED WEATHERING PRODUCT(67,2)|ACIDIFIED DRIED SOIL SAMPLE(64,6)|GROUND(61,39)|MOISTURE CONTENT(55,6)|CARBON DIOXIDE REMOVAL(50,4)|ENOUGH MOISTURE(50,1)|DROUGHT(46,1)|CENTRIFUGE SPENT CORE SOLUTION(45,2)|RAINFALL(44,2)|PORE WATER EXTRACTION(40,2)|PORE SOIL WATER(38,1)|TREATED DRIED SOIL SAMPLE(36,4)|RELIABLE DATA(36,1)|STERILIZED DISTILLED WATER BATH(33,3)|FACTOR CHANGE(30,2)|DRAINAGE(28,2)|AMMONIUM ACETATE SOLUTION(26,6)|MONTH NUMBER(26,1)|ENHANCED WEATHERING OPERATION(25,5)|ARTIFICIAL RAIN WATER(24,3)|GRAVEL(19,11)|WATER CONTENT(18,5)|OVEN(18,3)|PORE WATER(17,10)|ULTRAHIGH PURITY WATER(17,3)|CRUSHED ROCK GEOCHEMICAL(16,1)|SOIL CORE SAMPLE CONTAINER(14,6)|MOISTURE PROBE(14,2)|NITRIC ACID(14,2)|MACRO RHYZON(14,1)|EXTRACTING WATER CONTENT(12,3)|ENHANCING SOIL(11,2)|FARM MACHINERY(10,3)|ANALYTICAL GRADE AMMONIUM ACETATE(10,1)|ANALYTICAL GRADE AMMONIUM HYDROXIDE(10,1)|MEASUREMENT OPTION(10,1)|ROCK PARTICLE(10,1)|TOTAL CATION QUANTIFICATION(10,1)|TREATED SPENT CORE(10,1)|RPM(9,4)|SEA(9,3)|BICARBONATE(8,2)|CARBON DIOXIDE CAPTURE(8,2)|TRAILER(8,2)|ANALYTICAL GRADE ACETIC ACID(8,1)|CATION CONTENT(8,1)|CENTRIFUGE EQUIPMENT(8,1)|DISPERSION(8,1)|ENHANCED WEATHERING OPERATOR(8,1)|MODELED CARBON CAPTURE(8,1)|PARAMETER CALCULATION(8,1)|SAMPLE DRY LAND(8,1)|SPREADING CRUSHED SILICATE(8,1)|STANDARD CENTRIFUGE(8,1)|ULTRA HIGH PURITY WATER(8,1)|BOTTOM LID(6,3)|ADDING CRUSHED ROCK(6,1)|ALKALINITY(6,1)|BASALT(6,1)|CENTRIFUGATION(6,1)|ENHANCED WEATHERING PERFORMANCE(6,1)|ENHANCED WEATHERING REACTION(6,1)|FASTENING(6,1)|LABORATORY(6,1)||(GB2636853)|SOIL SAMPLE(100,58)|CARBON DIOXIDE(100,15)|ENHANCED WEATHERING(100,9)|PORE WATER SAMPLE(100,4)|ENHANCED WEATHERING CARBON DIOXIDE(100,1)|REMOVAL QUANTIFICATION(100,1)|ENOUGH MOISTURE(38,1)|GROUND(36,31)|DROUGHT(35,1)|RAINFALL(33,2)|ENHANCED WEATHERING PRODUCT(32,1)|MOISTURE CONTENT(30,5)|PORE SOIL WATER(29,1)|RELIABLE DATA(27,1)|STERILIZED DISTILLED WATER BATH(25,3)|DRAINAGE(21,2)|MONTH NUMBER(20,1)|CARBON DIOXIDE REMOVAL(19,2)|ARTIFICIAL RAIN WATER(18,3)|GRAVEL(14,11)|WATER CONTENT(13,5)|CRUSHED ROCK GEOCHEMICAL(12,1)|ENHANCED WEATHERING OPERATION(10,4)|MOISTURE PROBE(10,2)|MACRO RHYZON(10,1)|PORE WATER(9,9)|EXTRACTING WATER CONTENT(9,3)|FARM MACHINERY(7,3)|SEA(7,3)|MEASUREMENT OPTION(7,1)|ROCK PARTICLE(7,1)|BICARBONATE(6,2)|CARBON DIOXIDE CAPTURE(6,2)|TRAILER(6,2)|1M HCL(6,1)|CATION CONTENT(6,1)|CENTRIFUGE EQUIPMENT(6,1)|DISPERSION(6,1)|ENHANCED WEATHERING OPERATOR(6,1)|ENHANCING SOIL(6,1)|MODELED CARBON CAPTURE(6,1)|PARAMETER CALCULATION(6,1)|SAMPLE DRY LAND(6,1)|SPREADING CRUSHED SILICATE(6,1)|STANDARD CENTRIFUGE(6,1)|BOTTOM LID(5,3)|ADDING CRUSHED ROCK(4,1)|ALKALINITY(4,1)|BASALT(4,1)|ENHANCED WEATHERING PERFORMANCE(4,1)|ENHANCED WEATHERING REACTION(4,1)|FASTENING(4,1)|LABORATORY(4,1)|NEIGHBORING WATER MOLECULE(4,1)|OUTGASSING(4,1)|QUANTIFICATION(4,1)| (WO2025/133560)|CLAIMS: |1. A method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).|2. The method of any preceding claim, wherein the soil sample is contained in a sample tube.|3. The method of claim 2 wherein the sample tube is substantially made from metal and/or is substantially cylindrical.|4. The method of either claims 2 or 3 wherein the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube.|5. The method of any preceding claim, wherein the bath of water comprises a bath of sterilised distilled water.|6. The method of any preceding claim, wherein the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius.|7. The method of any preceding claim, wherein the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage.|8. The method of any preceding claim, wherein the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge.|9. The method of claim 8 wherein the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.|10. The method of any preceding claim further comprising the step of filtering the extracted water content.|11. The method of claim 10 wherein the step of filtering is performed for substantially 5 to 10 minutes.|12. The method of any preceding claim further comprising: drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample.|13. The method of claim 12 wherein drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample.|14. The method of claims 12 or 13 further comprising the step of placing the dried soil sample in a rotating shaking apparatus.|15. The method of any of claims 12 to 14, wherein applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution.|16. The method of any of claims 12 to 15 wherein the acid is nitric acid.|17. The method of any of claims 12 to 16 wherein the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra- high purity water. (WO2025/133560)|[0001] ENHANCED WEATHERING CARBON DIOXIDE REMOVAL QUANTIFICATION METHOD AND APPARATUS | [0002] Field | [0003] The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water. | [0004] Background | [0005] Enhanced weathering is the process of spreading suitable crushed silicate rock materials over suitable land, such as farmland. Suitable rock materials include rock such as basalt, which naturally reacts with dissolved carbon dioxide in the form of carbonic acid to remove the carbon dioxide from the environment. By crushing the rock, the crushed rock has a larger surface area per particle which speeds up the process of capturing carbon dioxide by increasing the reaction surface area. By spreading the rock over, for example, farmland, carbon dioxide can be captured over a large land surface. | [0006] During enhanced weathering, it is important to measure the properties of the enhanced weathering reaction in order to measure the amount of carbon dioxide captured in the soil, rivers and eventually oceans. This data can be used to compare against modelled carbon capture, verify carbon credits, or plan further enhanced weathering based on weathering performance. | [0007] To measure enhanced weathering, one of the measurement options is to extract pore water using a tool called a macro rhyzon in order to determine the level of carbon capture from the sample or samples is obtained. However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data. | [0008] Summary of Invention | [0009] Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. | [0010] According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removingthe soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850). | [0011] By allowing the soil sample to be placed in water, the soil sample can saturate with water and this can allow the subsequent removal of both the added water and the original water content for subsequent testing. This can allow the testing of water in a soil sample containing substantially too low a moisture content to provide sufficient water for normal pore water testing. | [0012] Optionally, the soil sample is contained in a sample tube. Optionally, the sample tube is substantially made from metal and/or is substantially cylindrical. Optionally, the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube. | [0013] The soil sample can be contained in a variety of configurations of sample apparatus, but can typically be obtained using a configuration of sample apparatus that is operable to work with a standard centrifuge and/or standard configuration of mechanical pressure apparatus. | [0014] Optionally, the bath of water comprises a bath of sterilised distilled water. | [0015] In other embodiments, artificial rainwater can be used. Using sterilised distilled water and/or artificial rainwater can allow the extracted water content to retain substantially all of the properties desired to be measured. | [0016] Optionally, the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius. | [0017] Placing the soil sample in a bath of water under substantially these conditions can allow the soil sample to saturate with the water contained in the bath and/or substantially not change the properties of the soil sample and/or its water content. | [0018] Optionally, the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage. | [0019] Removing the soil sample from the bath of water can allow only water that has been absorbed by the soil sample to remain prior to further step of the process being performed. | [0020] Optionally, the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge. | [0021] Placing the soil sample in a centrifuge can remove the moisture content of the soil substantially quickly, and/or causes water molecules being removed from the soil sample during the centrifuge operation to pull neighbouring water molecules out of the soil sample. | [0022] Optionally, the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.Using this configuration of centrifuge equipment can allow sufficient water to be removed from the soil sample to allow subsequent tests to be performed on a substantially sufficient sample size. | [0023] Optionally, the method further comprises the step of filtering the extracted water content. Optionally, the step of filtering is performed for substantially 5 to 10 minutes. | [0024] By filtering the water, debris such as soil can be removed which might otherwise impact the measurements/analysis performed on the extracted water. | [0025] Optionally, the method further comprises drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample. Optionally drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample. Optionally, the method further comprises the step of placing the dried soil sample in a rotating shaking apparatus. Optionally applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution. Optionally the acid is nitric acid. Optionally, the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra-high purity water. | [0026] By treating the “spent core” samples using ammonium acetate solution and analysing the treated spent cores, it is possible to measure the cations in the spent core and therefore at the site from which the core was obtained. | [0027] Brief Description of Drawings | [0028] Embodiments will now be described, by way of example only and with reference to the accompanying drawings having like-reference numerals, in which: | [0029] Figure 1 shows an example enhanced weathering process; | [0030] Figure 2 shows an example of a soil core sample container; | [0031] Figure 3 shows an example of the use of the soil core sample container, prior to insertion into the soil to be sampled; | [0032] Figure 4 shows an example of the use of the soil core sample container to insert into the soil to be sampled; | [0033] Figure 5 shows an example of the use of the soil core sample container being removed from the soil to be sampled;Figure 6 shows an example of the use of the soil core sample container to contain the soil to be sampled; | [0034] Figure 7 shows an example of the use of the soil core sample container being secured for transport with the soil sample inside; and | [0035] Figure 8 shows an embodiment of the enhanced soil core moisture process. | [0036] Specific Description | [0037] Referring to Figure 1 , an example of an enhanced weathering process 100 will now be described. | [0038] Enhanced weathering is performed by adding crushed rock 130 to farmland 140. In this described embodiment, the crushed rock 130 is added using farm machinery 120 such as a tractor with a trailer containing the crushed rock 130, where the trailer is configured to disperse the crushed rock 130 in a predetermined dispersal rate over substantially all of the surface of the farmland 140 as the farm machinery 120 travels along the farmland 140, typically travelling along parallel lines back and forth along the farmland 140. | [0039] Not all of the land needs to be subject to enhanced weathering, so in this embodiment farmland 140 undergoes the enhanced weathering process 100 but non-weathered land 110 does not have any crushed rock 130 spread over its surface. | [0040] In this embodiment, the properties of the farmland 140 that is to be subject to the enhanced weathering process 100 are determined in advance based on a combination of data for the area in which the farmland 140 is located along with data collected from the farmland 140. This data includes expected rainfall, pH, soil composition. Other data that is used as part of the process 100 is data pertaining to the crushed rock 130, including geochemical properties of the crushed rock and the range of surface area of the rock particles. Using this data, the amount of crushed rock 130 to spread over the farmland 140 and the density of spread/amount to be spread over the farmland 140 is calculated in advance of the spreading operation by the farm machinery 120. | [0041] In other embodiments, different data can be obtained in advance of the spreading operation. In other embodiments, a spreading plan can comprise different arrangements for different parts of the farmland 140, for example differing amounts of rock to be spread on different portions of the farmland 140. In other embodiments, different equipment can be used to spread the crushed rock 130. In other embodiments, multiple spreading operations may be performed at one or more time intervals. In other embodiments, sensors can be used to monitor the properties of the farmland 140, before and/or after the one or more spreading operations being performed.Following the enhanced weathering operation 100, carbon dioxide is absorbed from the atmosphere above the farmland 140 by a chemical reaction between the dissolved carbon dioxide and the crushed rock 130 spread over the surface of the farmland 140. This captures and sequesters carbon dioxide from the atmosphere into the soil over substantially the entire area that has been subject to enhanced weathering operations 100. Depending on the parameters that have been calculated for the rock spreading operation(s), the rate of carbon dioxide capture depends on the amount and properties of the crushed rock 130 that has been spread over the farmland 140 and a prediction for this carbon dioxide capture will be determined from the calculated parameters for the rock spreading operation(s). | [0042] Following the enhanced weathering operation 100, one of the measurements that needs to be performed to verify the amount of carbon captured is to measure the properties of the water in the soil, specifically the pore water. Pore water measurements can be key to understanding the soil chemistry and therefore how much carbon dioxide has been removed from the atmosphere. Enhanced weathering performance can depend on the pore water leaving the soil via the normal channels (e.g. streams and rivers) and reaching the ocean. Therefore, operators of enhanced weathering processes typically measure the contents of water in fields undergoing enhanced weathering to demonstrate bicarbonate and cation content in the pore water, which then leaves the soil and in time enters the ocean. | [0043] Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water. If this is the case then the following process can be used to obtain sufficient water from soil that contains too little moisture. | [0044] Pore water samples also should be analysed within around 36 hours of taking the sample, as the partial pressure of carbon dioxide in soil is different to that in air, so over time there is outgassing and degradation of the data (e.g. the bicarbonates in the soil sample will typically degrade over time as the pressure equilibrium moves from that of soil to that of air) that can be obtained from the pore water if tests aren’t performed promptly. | [0045] Simply applying a large degree of pressure to the soil samples may not be possible is the moisture content is too low, as there is a limit to the amount of mechanical suction/pressure that is possible and depending on the type of soil it becomes impossible to extract sufficient water once the moisture levels drop below a certain level (this level varies by soil composition). Some methods of suction/pressure can extract sufficient water from soil samples but take too long, and after 36 hours from taking the soil sample the water extracted doesn’t provide a representative sample for analysis. | [0046] Referring to Figure 2, an example soil core sample container 200 will now be described.The sample tube 220 is a hollow metal cylinder, which has two caps or lids, a top lid 210 and a bottom lid 230. The top and bottom lids 210, 230 are designed to fit on to the open ends of the tube 220 to secure and seal the sample soil contained within the sample tube 220. In this embodiment the caps 210, 230 fit to the ends of the tube 220 by an interference fit. In other embodiments, the caps 210, 230 can use a screw thread to fit to the tube 220. In other embodiments, other fixing mechanisms can be used to secure the lids 210, 230 to the tube 220. In this embodiment, each cylinder has a 5cm diameter and is 5cm deep. | [0047] Typically, in this embodiment, multiple samples will be taken each with separate soil core sample containers, commensurate to the area of land being sampled. | [0048] Referring to Figure 3, an example of use 300 of the soil core container of Figure 2 will now be described. | [0049] A sample tube 310 (as described above in relation to Figure 2) is shown in this embodiment without caps. It is positioned above the surface of the soil 320. The intention is to sample a core of soil by inserting the sample tube 310 into the soil surface 320 to obtain a core of soil within the sample tube 310. | [0050] Referring to Figure 4, an example of soil sampling 400 using the soil core container of Figure 2 will now be described. | [0051] The sample tube 410 is inserted 440 into the soil, penetrating the soil surface 420 and thereby causing a sample of soil 430 to enter into the sample tube 410. In this embodiment, the tube 410 is hammered into the soil. | [0052] Referring to Figure 5, an example of soil sample removal 500 using the soil core container of Figure 2 will now be described. | [0053] The sample tube 510 is removed 540 from the soil surface 520, leaving a hole 550 and with the soil sample 530 contained within the sample tube 510. The soil sample 530 typically stays within the sample tube 510 when it is removed from the ground. It is typically very important to keep the soil core as a solid undisturbed soil sample hence it is kept intact within the cylinder 510. | [0054] Referring to Figure 6, an example of securing the soil 600 within the soil core container of Figure 2 will now be described. | [0055] The sample tube 610 containing the soil sample 630 then has the two lids 620, 640 placed at either open end of the cylinder 610 containing the soil sample 630. | [0056] The top lid 620 is fit over one end of the sample tube 610 using an interference fit. The bottom lid 640 is fit over the other end of the sample tube 610 using an interference fit. The lids 620, 640 prevent the soil or any moisture from leaving the interior of the sample tube 610. | [0057] In other embodiments, other fastening mechanisms can be used to fasten the lids 620, 640 to the tube 610.Referring to Figure 7, an example of readying the soil sample for transport 700 using the soil core container of Figure 2 will now be described. | [0058] The sample tube 710 is shown with both lids 720, 740 securely fastened over either open end of the cylinder 710 containing the soil sample 730. The soil sample 730 is able to be transported securely within the sample tube 710, for example to a laboratory for testing the contents of the tube 710. | [0059] Referring to Figure 8, an embodiment of the enhanced soil core moisture process 800 will now be described. | [0060] In a first step 810, the soil sample in the sample tube is received 810. Typically this will be in a laboratory-setting with equipment to analyse the contents of the sample tube. | [0061] In a second step 820, the soil sample tube has at least one lid removed and the open side of the tube is placed in a bath of sterilised distilled water. In this embodiment, each sample is saturated in 60ml of sterilised distilled water. | [0062] In this embodiment, 60ml of sterilised distilled water should be sufficient for the soil sample size (using a 5cm diameter and 5cm deep cylinder) not to dilute the “signal” being analysed when testing the water extracted at the end of the process of this embodiment. | [0063] In this embodiment, de-ionised water or very pure water is not used to prevent the soil leaching some of its contents into the bath of water (which will alter the subsequent analysis data detrimentally). In some embodiments, artificial rainwater can be used. | [0064] In a third step 830, the sample tube is left for 24 hours at 2-4 degrees Celsius to saturate with the sterilised distilled water. | [0065] In a fourth step 840, the sample tube is removed from the bath of water in order to allow free drainage of any water that hasn’t soaked into the soil sample in the tube. | [0066] In a fifth step 850, the sample is placed into a centrifuge and spun for thirty minutes at 1 ,000 revolutions per minute in order to extract the water from the soil sample. The water is collected by the equipment. Typically about 20-30ml will be collected from each soil sample. | [0067] In a sixth step 860, the water collected by the centrifuge is filtered for five to ten minutes. This filtered water can then be processed as would a normal pore water sample where the soil sample contains sufficient moisture. The filtration aims to remove for example small pieces of soil. In some embodiments, the filtration step could occur earlier by for example placing filter paper at at least one (or both) sides of the cylinder containing the soil sample. | [0068] Measurements in this embodiment are then taken of alkalinity, pH and EC. In some embodiments, any or any combination of the following measurements as follows can be taken: pH using a benchtop pH meter; EC using a benchtop EC meter; alkalinity using titration using 0.1 M HCL; cations using ICP-AES; anions using IC. | [0069] After centrifugation and pore water extraction, the core/soil samples are considered ‘spent’. Optionally, in some embodiments, the 'spent cores' are then slowly air dried in an ovenbefore being crushed, mixed and sieved in preparation for an ammonium acetate leach. In an embodiment, 2g of the dried soil is combined with ammonium acetate solution (in this embodiment, analytical grade NH4OAc ammonium acetate is used, with a formula weight of 77.08g/mol) before being placed into a rotating shaker for 2 hours at room temperature. The sample is then centrifuged in either 15ml or 50ml centrifuge tubes for 10 minutes at 4000 RPM before being allowed to settle for 10 mins. The solution is extracted and filtered before being acidified with nitric acid (in this embodiment, analytical grade HNO3 nitric acid, with a formula weight of 63.01 g/mol, is used). The filtered and acidified solution is sent to analysis by ICP- MS. This method allows a quantification of total cations held on the soil exchange sites. | [0070] In the example embodiment, the ammonium acetate solution comprises a mixture of analytical grade ammonium acetate (NH4OAc; Formula weight = 77.08 g/mol); analytical grade ammonium hydroxide (NH4OH; Formula weight = 35.04 g/mol); analytical grade acetic acid (CH3COOH; Formula weight = 60.05 g/mol); and ultra-high purity water. The ammonium acetate and ultra-high purity water are mixed first, to create a 1M solution. The pH of the solution is then measured in order to then adjust the pH of the solution to pH8.5, by either adding acetic acid to lower the pH or by adding ammonium hydroxide to raise the pH of the solution. | [0071] In some embodiments, a moisture probe can be used in the soil to be sample prior to take soil core samples and the data from the moisture probe can be used to determine how much water should be contained in the water bath in order to determine how much the pore water sample is diluted by the saturation step in process 800. | [0072] In some embodiments, in place of a centrifuge, a mechanical pressure device can be used such as a hydraulic press. | [0073] Any system feature as described herein may also be provided as a method feature, and vice versa. As used herein, means plus function features may be expressed alternatively in terms of their corresponding structure. | [0074] Any feature in one aspect may be applied to other aspects, in any appropriate combination. In particular, method aspects may be applied to system aspects, and vice versa. Furthermore, any, some and/or all features in one aspect can be applied to any, some and/or all features in any other aspect, in any appropriate combination. | [0075] It should also be appreciated that particular combinations of the various features described and defined in any aspects can be implemented and/or supplied and/or used independently. (WO2025/133560)|[0001] ENHANCED WEATHERING CARBON DIOXIDE REMOVAL QUANTIFICATION METHOD AND APPARATUS | [0002] Field | [0003] The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water. | [0004] Background | [0005] Enhanced weathering is the process of spreading suitable crushed silicate rock materials over suitable land, such as farmland. Suitable rock materials include rock such as basalt, which naturally reacts with dissolved carbon dioxide in the form of carbonic acid to remove the carbon dioxide from the environment. By crushing the rock, the crushed rock has a larger surface area per particle which speeds up the process of capturing carbon dioxide by increasing the reaction surface area. By spreading the rock over, for example, farmland, carbon dioxide can be captured over a large land surface. | [0006] During enhanced weathering, it is important to measure the properties of the enhanced weathering reaction in order to measure the amount of carbon dioxide captured in the soil, rivers and eventually oceans. This data can be used to compare against modelled carbon capture, verify carbon credits, or plan further enhanced weathering based on weathering performance. | [0007] To measure enhanced weathering, one of the measurement options is to extract pore water using a tool called a macro rhyzon in order to determine the level of carbon capture from the sample or samples is obtained. However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data. | [0008] Summary of Invention | [0009] Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. | [0010] According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removingthe soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850). | [0011] By allowing the soil sample to be placed in water, the soil sample can saturate with water and this can allow the subsequent removal of both the added water and the original water content for subsequent testing. This can allow the testing of water in a soil sample containing substantially too low a moisture content to provide sufficient water for normal pore water testing. | [0012] Optionally, the soil sample is contained in a sample tube. Optionally, the sample tube is substantially made from metal and/or is substantially cylindrical. Optionally, the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube. | [0013] The soil sample can be contained in a variety of configurations of sample apparatus, but can typically be obtained using a configuration of sample apparatus that is operable to work with a standard centrifuge and/or standard configuration of mechanical pressure apparatus. | [0014] Optionally, the bath of water comprises a bath of sterilised distilled water. | [0015] In other embodiments, artificial rainwater can be used. Using sterilised distilled water and/or artificial rainwater can allow the extracted water content to retain substantially all of the properties desired to be measured. | [0016] Optionally, the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius. | [0017] Placing the soil sample in a bath of water under substantially these conditions can allow the soil sample to saturate with the water contained in the bath and/or substantially not change the properties of the soil sample and/or its water content. | [0018] Optionally, the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage. | [0019] Removing the soil sample from the bath of water can allow only water that has been absorbed by the soil sample to remain prior to further step of the process being performed. | [0020] Optionally, the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge. | [0021] Placing the soil sample in a centrifuge can remove the moisture content of the soil substantially quickly, and/or causes water molecules being removed from the soil sample during the centrifuge operation to pull neighbouring water molecules out of the soil sample. | [0022] Optionally, the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.Using this configuration of centrifuge equipment can allow sufficient water to be removed from the soil sample to allow subsequent tests to be performed on a substantially sufficient sample size. | [0023] Optionally, the method further comprises the step of filtering the extracted water content. Optionally, the step of filtering is performed for substantially 5 to 10 minutes. | [0024] By filtering the water, debris such as soil can be removed which might otherwise impact the measurements/analysis performed on the extracted water. | [0025] Optionally, the method further comprises drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample. Optionally drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample. Optionally, the method further comprises the step of placing the dried soil sample in a rotating shaking apparatus. Optionally applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution. Optionally the acid is nitric acid. Optionally, the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra-high purity water. | [0026] By treating the “spent core” samples using ammonium acetate solution and analysing the treated spent cores, it is possible to measure the cations in the spent core and therefore at the site from which the core was obtained. | [0027] Brief Description of Drawings | [0028] Embodiments will now be described, by way of example only and with reference to the accompanying drawings having like-reference numerals, in which: | [0029] Figure 1 shows an example enhanced weathering process; | [0030] Figure 2 shows an example of a soil core sample container; | [0031] Figure 3 shows an example of the use of the soil core sample container, prior to insertion into the soil to be sampled; | [0032] Figure 4 shows an example of the use of the soil core sample container to insert into the soil to be sampled; | [0033] Figure 5 shows an example of the use of the soil core sample container being removed from the soil to be sampled;Figure 6 shows an example of the use of the soil core sample container to contain the soil to be sampled; | [0034] Figure 7 shows an example of the use of the soil core sample container being secured for transport with the soil sample inside; and | [0035] Figure 8 shows an embodiment of the enhanced soil core moisture process. | [0036] Specific Description | [0037] Referring to Figure 1 , an example of an enhanced weathering process 100 will now be described. | [0038] Enhanced weathering is performed by adding crushed rock 130 to farmland 140. In this described embodiment, the crushed rock 130 is added using farm machinery 120 such as a tractor with a trailer containing the crushed rock 130, where the trailer is configured to disperse the crushed rock 130 in a predetermined dispersal rate over substantially all of the surface of the farmland 140 as the farm machinery 120 travels along the farmland 140, typically travelling along parallel lines back and forth along the farmland 140. | [0039] Not all of the land needs to be subject to enhanced weathering, so in this embodiment farmland 140 undergoes the enhanced weathering process 100 but non-weathered land 110 does not have any crushed rock 130 spread over its surface. | [0040] In this embodiment, the properties of the farmland 140 that is to be subject to the enhanced weathering process 100 are determined in advance based on a combination of data for the area in which the farmland 140 is located along with data collected from the farmland 140. This data includes expected rainfall, pH, soil composition. Other data that is used as part of the process 100 is data pertaining to the crushed rock 130, including geochemical properties of the crushed rock and the range of surface area of the rock particles. Using this data, the amount of crushed rock 130 to spread over the farmland 140 and the density of spread/amount to be spread over the farmland 140 is calculated in advance of the spreading operation by the farm machinery 120. | [0041] In other embodiments, different data can be obtained in advance of the spreading operation. In other embodiments, a spreading plan can comprise different arrangements for different parts of the farmland 140, for example differing amounts of rock to be spread on different portions of the farmland 140. In other embodiments, different equipment can be used to spread the crushed rock 130. In other embodiments, multiple spreading operations may be performed at one or more time intervals. In other embodiments, sensors can be used to monitor the properties of the farmland 140, before and/or after the one or more spreading operations being performed.Following the enhanced weathering operation 100, carbon dioxide is absorbed from the atmosphere above the farmland 140 by a chemical reaction between the dissolved carbon dioxide and the crushed rock 130 spread over the surface of the farmland 140. This captures and sequesters carbon dioxide from the atmosphere into the soil over substantially the entire area that has been subject to enhanced weathering operations 100. Depending on the parameters that have been calculated for the rock spreading operation(s), the rate of carbon dioxide capture depends on the amount and properties of the crushed rock 130 that has been spread over the farmland 140 and a prediction for this carbon dioxide capture will be determined from the calculated parameters for the rock spreading operation(s). | [0042] Following the enhanced weathering operation 100, one of the measurements that needs to be performed to verify the amount of carbon captured is to measure the properties of the water in the soil, specifically the pore water. Pore water measurements can be key to understanding the soil chemistry and therefore how much carbon dioxide has been removed from the atmosphere. Enhanced weathering performance can depend on the pore water leaving the soil via the normal channels (e.g. streams and rivers) and reaching the ocean. Therefore, operators of enhanced weathering processes typically measure the contents of water in fields undergoing enhanced weathering to demonstrate bicarbonate and cation content in the pore water, which then leaves the soil and in time enters the ocean. | [0043] Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water. If this is the case then the following process can be used to obtain sufficient water from soil that contains too little moisture. | [0044] Pore water samples also should be analysed within around 36 hours of taking the sample, as the partial pressure of carbon dioxide in soil is different to that in air, so over time there is outgassing and degradation of the data (e.g. the bicarbonates in the soil sample will typically degrade over time as the pressure equilibrium moves from that of soil to that of air) that can be obtained from the pore water if tests aren’t performed promptly. | [0045] Simply applying a large degree of pressure to the soil samples may not be possible is the moisture content is too low, as there is a limit to the amount of mechanical suction/pressure that is possible and depending on the type of soil it becomes impossible to extract sufficient water once the moisture levels drop below a certain level (this level varies by soil composition). Some methods of suction/pressure can extract sufficient water from soil samples but take too long, and after 36 hours from taking the soil sample the water extracted doesn’t provide a representative sample for analysis. | [0046] Referring to Figure 2, an example soil core sample container 200 will now be described.The sample tube 220 is a hollow metal cylinder, which has two caps or lids, a top lid 210 and a bottom lid 230. The top and bottom lids 210, 230 are designed to fit on to the open ends of the tube 220 to secure and seal the sample soil contained within the sample tube 220. In this embodiment the caps 210, 230 fit to the ends of the tube 220 by an interference fit. In other embodiments, the caps 210, 230 can use a screw thread to fit to the tube 220. In other embodiments, other fixing mechanisms can be used to secure the lids 210, 230 to the tube 220. In this embodiment, each cylinder has a 5cm diameter and is 5cm deep. | [0047] Typically, in this embodiment, multiple samples will be taken each with separate soil core sample containers, commensurate to the area of land being sampled. | [0048] Referring to Figure 3, an example of use 300 of the soil core container of Figure 2 will now be described. | [0049] A sample tube 310 (as described above in relation to Figure 2) is shown in this embodiment without caps. It is positioned above the surface of the soil 320. The intention is to sample a core of soil by inserting the sample tube 310 into the soil surface 320 to obtain a core of soil within the sample tube 310. | [0050] Referring to Figure 4, an example of soil sampling 400 using the soil core container of Figure 2 will now be described. | [0051] The sample tube 410 is inserted 440 into the soil, penetrating the soil surface 420 and thereby causing a sample of soil 430 to enter into the sample tube 410. In this embodiment, the tube 410 is hammered into the soil. | [0052] Referring to Figure 5, an example of soil sample removal 500 using the soil core container of Figure 2 will now be described. | [0053] The sample tube 510 is removed 540 from the soil surface 520, leaving a hole 550 and with the soil sample 530 contained within the sample tube 510. The soil sample 530 typically stays within the sample tube 510 when it is removed from the ground. It is typically very important to keep the soil core as a solid undisturbed soil sample hence it is kept intact within the cylinder 510. | [0054] Referring to Figure 6, an example of securing the soil 600 within the soil core container of Figure 2 will now be described. | [0055] The sample tube 610 containing the soil sample 630 then has the two lids 620, 640 placed at either open end of the cylinder 610 containing the soil sample 630. | [0056] The top lid 620 is fit over one end of the sample tube 610 using an interference fit. The bottom lid 640 is fit over the other end of the sample tube 610 using an interference fit. The lids 620, 640 prevent the soil or any moisture from leaving the interior of the sample tube 610. | [0057] In other embodiments, other fastening mechanisms can be used to fasten the lids 620, 640 to the tube 610.Referring to Figure 7, an example of readying the soil sample for transport 700 using the soil core container of Figure 2 will now be described. | [0058] The sample tube 710 is shown with both lids 720, 740 securely fastened over either open end of the cylinder 710 containing the soil sample 730. The soil sample 730 is able to be transported securely within the sample tube 710, for example to a laboratory for testing the contents of the tube 710. | [0059] Referring to Figure 8, an embodiment of the enhanced soil core moisture process 800 will now be described. | [0060] In a first step 810, the soil sample in the sample tube is received 810. Typically this will be in a laboratory-setting with equipment to analyse the contents of the sample tube. | [0061] In a second step 820, the soil sample tube has at least one lid removed and the open side of the tube is placed in a bath of sterilised distilled water. In this embodiment, each sample is saturated in 60ml of sterilised distilled water. | [0062] In this embodiment, 60ml of sterilised distilled water should be sufficient for the soil sample size (using a 5cm diameter and 5cm deep cylinder) not to dilute the “signal” being analysed when testing the water extracted at the end of the process of this embodiment. | [0063] In this embodiment, de-ionised water or very pure water is not used to prevent the soil leaching some of its contents into the bath of water (which will alter the subsequent analysis data detrimentally). In some embodiments, artificial rainwater can be used. | [0064] In a third step 830, the sample tube is left for 24 hours at 2-4 degrees Celsius to saturate with the sterilised distilled water. | [0065] In a fourth step 840, the sample tube is removed from the bath of water in order to allow free drainage of any water that hasn’t soaked into the soil sample in the tube. | [0066] In a fifth step 850, the sample is placed into a centrifuge and spun for thirty minutes at 1 ,000 revolutions per minute in order to extract the water from the soil sample. The water is collected by the equipment. Typically about 20-30ml will be collected from each soil sample. | [0067] In a sixth step 860, the water collected by the centrifuge is filtered for five to ten minutes. This filtered water can then be processed as would a normal pore water sample where the soil sample contains sufficient moisture. The filtration aims to remove for example small pieces of soil. In some embodiments, the filtration step could occur earlier by for example placing filter paper at at least one (or both) sides of the cylinder containing the soil sample. | [0068] Measurements in this embodiment are then taken of alkalinity, pH and EC. In some embodiments, any or any combination of the following measurements as follows can be taken: pH using a benchtop pH meter; EC using a benchtop EC meter; alkalinity using titration using 0.1 M HCL; cations using ICP-AES; anions using IC. | [0069] After centrifugation and pore water extraction, the core/soil samples are considered ‘spent’. Optionally, in some embodiments, the 'spent cores' are then slowly air dried in an ovenbefore being crushed, mixed and sieved in preparation for an ammonium acetate leach. In an embodiment, 2g of the dried soil is combined with ammonium acetate solution (in this embodiment, analytical grade NH4OAc ammonium acetate is used, with a formula weight of 77.08g/mol) before being placed into a rotating shaker for 2 hours at room temperature. The sample is then centrifuged in either 15ml or 50ml centrifuge tubes for 10 minutes at 4000 RPM before being allowed to settle for 10 mins. The solution is extracted and filtered before being acidified with nitric acid (in this embodiment, analytical grade HNO3 nitric acid, with a formula weight of 63.01 g/mol, is used). The filtered and acidified solution is sent to analysis by ICP- MS. This method allows a quantification of total cations held on the soil exchange sites. | [0070] In the example embodiment, the ammonium acetate solution comprises a mixture of analytical grade ammonium acetate (NH4OAc; Formula weight = 77.08 g/mol); analytical grade ammonium hydroxide (NH4OH; Formula weight = 35.04 g/mol); analytical grade acetic acid (CH3COOH; Formula weight = 60.05 g/mol); and ultra-high purity water. The ammonium acetate and ultra-high purity water are mixed first, to create a 1M solution. The pH of the solution is then measured in order to then adjust the pH of the solution to pH8.5, by either adding acetic acid to lower the pH or by adding ammonium hydroxide to raise the pH of the solution. | [0071] In some embodiments, a moisture probe can be used in the soil to be sample prior to take soil core samples and the data from the moisture probe can be used to determine how much water should be contained in the water bath in order to determine how much the pore water sample is diluted by the saturation step in process 800. | [0072] In some embodiments, in place of a centrifuge, a mechanical pressure device can be used such as a hydraulic press. | [0073] Any system feature as described herein may also be provided as a method feature, and vice versa. As used herein, means plus function features may be expressed alternatively in terms of their corresponding structure. | [0074] Any feature in one aspect may be applied to other aspects, in any appropriate combination. In particular, method aspects may be applied to system aspects, and vice versa. Furthermore, any, some and/or all features in one aspect can be applied to any, some and/or all features in any other aspect, in any appropriate combination. | [0075] It should also be appreciated that particular combinations of the various features described and defined in any aspects can be implemented and/or supplied and/or used independently. Family Number|(108540136)|108540136|Abstract|(GB2636853 A)|A method for quantifying carbon dioxide removal when performing enhance weathering operations. Measurements are enabled by taking soil cores 810, placing the core sample into a water bath, 820, leave sample to saturate 830, drain sample 840, apply pressure on the sample 850 to allow a pore sample of water to be extracted from the soil sample 860. Filtering may be carried out on the pore water sample during collection. Thus, pore water samples may be extracted from soil that may not have enough moisture to extract a sufficiently large enough pore sample. The method may then be used to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. Enhanced weathering is a process of spreading suitable crushed silicate rock materials over land such as farmland enabling carbon dioxide to be captured over a large area.|(WO2025133560 A1)|La présente invention concerne des procédés de quantification de l'élimination de dioxyde de carbone et de facteurs/changements associés lors de la réalisation d'opérations d'altération forcée. Plus particulièrement, la présente invention implique le fait de permettre la prise de mesures à partir de carottes de sol de produits d'altération forcée par extraction d'eau interstitielle. Des aspects et/ou des modes de réalisation visent à fournir un procédé pour extraire suffisamment d'échantillons d'eau interstitielle du sol, même lorsque le sol a une faible teneur en humidité, afin de réaliser des mesures sur l'eau interstitielle, par exemple pour vérifier ou mesurer l'altération forcée aux fins de la quantification d'élimination de dioxyde de carbone.|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal.|CPC codes|(GB2636853 A)|G01N-001/28|G01N-033/24/6|G01N-033/24|(WO2025133560 A1)|G01N-001/28|G01N-033/24/6|G01N-033/24|IPC codes|(GB2636853 A)|G01N-001/28|G01N-033/24|(WO2025133560 A1)|G01N-033/24|Title|(GB202319995 D0)|Enhanced weathering carbon dioxide removal quantification method and apparatus|(GB2636853 A)|Enhanced weathering carbon dioxide removal quantification method and apparatus|(WO2025133560 A1)|Enhanced weathering carbon dioxide removal quantification method and apparatus|Procédé et appareil de quantification d'élimination de dioxyde de carbone par altération forcée| Analysis of biological materials G01N-001/28|G01N-033/24|G01N-033/24/6 G01N-001/28|G01N-033/24|G01N-033/24/6 G01N-001/28|G01N-033/24 G01N-001/28|G01N-033/24 US20120103077|CN115307977|CN112525630|CN203772616U US20120103077 44414932 WHO=Examiner SELF=N CAT=A|CN115307977 102493973 WHO=Examiner SELF=N|CN112525630 93215294 WHO=Examiner SELF=N|CN203772616U 67217407 WHO=Examiner SELF=N XP091560179; XP086002247; US20120103077; XP037697290|CN203772616U; CN115307977; CN112525630 (WO2025/133560)|International Search Report [Examiner]|-DAVID J BEERLING ET AL: "Enhanced weathering in the U.S. Corn Belt delivers carbon removal with agronomic benefits", ARXIV.ORG, CORNELL UNIVERSITY LIBRARY, 201 OLIN LIBRARY CORNELL UNIVERSITY ITHACA, NY 14853, 6 July 2023 (2023-07-06), XP091560179|-LOZANO J C ET AL: "A system for obtaining soil solution extracts and soil water retention curves using a bench centrifuge with fixed angle rotors", GEODERMA, ELSEVIER, AMSTERDAM, NL, vol. 361, 27 November 2019 (2019-11-27), XP086002247, ISSN: 0016-7061, [retrieved on 20191127], DOI: 10.1016/J.GEODERMA.2019.114063|-LAUKKANEN JOHANNA ET AL: "In situ remediation of metal(loid)-contaminated lake sediments with alkali-activated blast furnace slag granule amendment: A field experiment", JOURNAL OF SOILS AND SEDIMENTS, SPRINGER, DE, vol. 22, no. 3, 26 January 2022 (2022-01-26), pages 1054 - 1067, XP037697290, ISSN: 1439-0108, [retrieved on 20220126], DOI: 10.1007/S11368-022-03140-Z|| PENDING (WO2025/133560)|PENDING|(GB2636853)|PENDING ALIVE (WO2025/133560)|ALIVE|(GB2636853)|ALIVE (WO2025/133560)|LEGAL DETAILS FOR WO2025/133560|Actual or expected expiration date=2027-06-22|Legal state=ALIVE|Status=PENDING|Event publication date=2024-07-08|Event code=WO/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=WO WOGB2024/051780|Application date=2024-07-08|Standardized application number=2024WO-GB51780|Event publication date=2025-06-26|Event code=WO/A1|Event group=Examination events|Published application with search report|Publication country=WO|Publication number=WO2025/133560|Publication stage code=A1|Publication date=2025-06-26|Standardized publication number=WO2025133560|Event publication date=2025-11-06|Event code=WO/DPE1|Event group=Examination events|Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)|MEMBER STATE LEGAL DETAILS FOR EP|Actual or expected expiration date=2044-07-08|Legal state=ALIVE|Status=PENDING|Corresponding cc:|Designated or member state=EP Corresponding appl: EP24743471|Event publication date=2025-08-06|Event code=WO/121|Event group=Designated states|EP: The EPO has been informed by wipo that ep was designated in this application|Corresponding cc:|Designated or member state=EP|(GB2636853)|LEGAL DETAILS FOR GB2636853|Actual or expected expiration date=2043-12-22|Legal state=ALIVE|Status=PENDING|Event publication date=2023-12-22|Event code=GB/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=GB GB202319995|Application date=2023-12-22|Standardized application number=2023GB-0019995|Event publication date=2024-02-07|Event code=GB/D0|Event indicator=Pos|Event group=Examination events|Patent application filed|Publication country=GB|Publication number=GB202319995|Publication stage code=D0|Publication date=2024-02-07|Standardized publication number=GB202319995|Event publication date=2025-07-02|Event code=GB/A|Event group=Examination events|Published Application|Publication country=GB|Publication number=GB2636853|Publication stage code=A|Publication date=2025-07-02|Standardized publication number=GB2636853 (WO2025/133560)|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW|(WO2025/133560)|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ|(WO2025/133560)|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR|(WO2025/133560)|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML|(WO2025/133560)|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (WO2025/133560)|WO; EP|(GB2636853)|GB https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCAiwlzxUQ66p90P/F2Pwh1EkaV0SMUACwOCCKReMmHu7M9Ry4MrhQjLALkMBz8hwaI=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006802716&ekey=2486&xpn=WO2025133560&kind=A1 http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2025133560&redirectedID=true https://permalink.orbit.com/RenderStaticFirstPage?XPN=OThLP3Yvv2mkh5CpoqtjpbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT GB (WO2025/133560)|GB (WO2025/133560)|NAME=UNDO CARBON LTD 3rd Floor 86-90 Paul Street London, EC2A 4NE , COUNTRY=GB (WO2025/133560)|GB (WO2025/133560)|NAME=BARNES IP LIMITED Castle Hill House 12 Castle Hill Windsor Berkshire SL4 1PD , POSTCODE=SL4 1PD , COUNTRY=GB (WO2025/133560)|GB| (WO2025/133560)|NAME=LIU, Xinran c/o Undo Carbon Ltd 3rd Floor 86-90 Paul Street London Greater London EC2A 4NE, POSTCODE=EC2A 4NE, COUNTRY=GB|(GB2636853)|NAME=Xinran Liu 7 2 Titre: (WO2025/133560)|Enhanced weathering carbon dioxide removal quantification method and apparatus Résumé: (WO2025/133560)|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. 12 Abstract gpt-4o-mini yes The article focuses on enhanced weathering operations aimed at quantifying carbon dioxide removal, which is central to the topic of accelerated weathering for CO₂ capture.
9 CN202510001550 CN202510001550 CN119929773 114438809 CN119929773 A 2025-05-06 [CN119929773] 2025-01-02 2025-01-02 2025-05-06 (CN119929773)|2045-01-02 (CN119929773)|Heavy salinized soil carbon sequestration and sink increasing and modifying agent as well as preparation method and application thereof (CN119929773)|The invention discloses a heavy salinized soil carbon sequestration and sink increasing and modifying agent as well as a preparation method and application of the heavy salinized soil carbon sequestration and sink increasing and modifying agent. The preparation method of the heavy salinized soil carbon sequestration and sink increasing and modifying agent comprises the following steps: collecting spartina alterniflora straws, crushing, performing high-temperature pyrolysis treatment for 40-80 minutes under the condition of 350-550 DEG C, and cooling to obtain spartina alterniflora biomass charcoal, namely the heavy salinized soil carbon sequestration and sink increasing and modifying agent. According to the method, the three targets of resource utilization of the waste straw, improvement of the coastal heavy salinized soil and carbon sequestration and carbon sink increase of the coastal heavy salinized wetland are achieved at the same time, the soil carbon reserve of the coastal wetland can be increased, and the carbon storage function of the wetland is greatly enhanced. NANJING NORMAL UNIVERSITY (CN119929773)|NANJING NORMAL UNIVERSITY ([CN]) LIU JINE|ZHANG WEITING|SONG GE|LUO XIN|LAI JIANPING|LIU HANZHONG|LIN XIAOWEN|SUN MINNAN (CN119929773)|LIU JINE|ZHANG WEITING|SONG GE|LUO XIN|LAI JIANPING|LIU HANZHONG|LIN XIAOWEN|SUN MINNAN (CN119929773)|ZHENG LIFA;NANJING ZHONGLV INTELLECTUAL PROPERTY AGENCY FRIM(GENERAL PARTNERSHIP)|Reg. Nb: 32341 (CN119929773)|The carbon-fixing and sink-increasing modifier for heavy salty soil, provided by the invention, and the preparation and application thereof, have the advantages of simple preparation, easily available raw materials and low cost.|But are limited by cost and application methods, often with limitations in practical use.|Therefore, the resource utilization of a large amount of spartina alterniflora straw generated by treatment becomes a main problem, and development of an environment-friendly method for realizing the resource utilization of spartina alterniflora is needed.| (CN119929773)|1. The preparation method of the carbon sequestration and sink enhancement and modifier for the heavy salty soil is characterized by comprising the following steps of: collecting spartina alterniflora straw, crushing, carrying out high-temperature pyrolysis treatment at 350-550 ℃ for 40-80min, and cooling to obtain spartina alterniflora biomass charcoal, namely the heavy saline soil carbon fixation and sequestration and modifier. | (CN119929773)|Aiming at the technical problems, the invention provides a carbon sequestration and exchange increasing and improving agent for heavy salty soil, and a preparation method and application thereof, which aim to regulate physicochemical properties of soil by preparing and adding the soil improving agent, indirectly change components and structures of organic carbon in the soil by the action of salt marsh plants and salt marsh microorganisms and improve carbon reserves of coastal carbon libraries.|The invention discloses a carbon sequestration and sink-increasing and modifying agent for heavy saline soil, a preparation method and application thereof, and belongs to the technical field of ecological environment improvement.|The invention discloses a carbon sequestration and sink-increasing and modifying agent for heavy saline soil, a preparation method and application thereof.| (CN119929773)|HEAVY SALTY SOIL(100,21)|CARBON SEQUESTRATION(100,20)|CARBON FIXATION(100,15)|SPARTINA ALTERNIFLORA BIOMASS CHARCOAL(100,8)|MODIFIER(100,7)|SPARTINA ALTERNIFLORA STRAW(84,13)|COLLECTING SPARTINA ALTERNIFLORA STRAW(78,3)|HEAVY SOIL SALINITY(51,16)|COASTAL HEAVY SALINE WETLAND(49,1)|REALIZING RESOURCE UTILIZATION(46,1)|WASTE STRAW RESOURCE UTILIZATION(40,1)|COASTAL CARBON LIBRARY(38,1)|SPARTINA ALTERNIFLORA STRAW POWDER(38,1)|SUAEDA SALSA(34,4)|HEAVY SALTED SOIL(33,4)|ECOLOGICAL ENVIRONMENT(31,1)|SALT MARSH MICROORGANISM(31,1)|SOIL PHYSICOCHEMICAL PROPERTY(31,1)|PYROLYSIS TREATMENT(30,7)|SEQUESTRATION(25,3)|RESOURCE UTILIZATION(25,2)|SPARTINA ALTERNIFLORA(24,17)|SEQUESTRATION IMPROVING AGENT(24,7)|SALTY PLANT(24,1)|SALINE SOIL CARBON FIXATION(22,5)|SALT MARSH PLANT ACTION(22,1)|ENVIRONMENT FRIENDLY DEVELOPMENT(21,1)|CRUSHING(18,4)|GROUND SURFACE(18,3)|SALT MARSH PLANT(18,2)|SINK INCREASING MODIFIER(18,1)|SOIL IMPROVING AGENT(18,1)|SOIL CARBON FIXATION(17,12)|SALINE SOIL IMPROVEMENT(16,1)|PHYSICOCHEMICAL PROPERTY(15,5)|PHRAGMITES AUSTRALIS(13,2)|NUTRIENT CONTENT(12,4)|GROUND(11,33)|CARBON FIXING(11,5)|SOIL HYDROLASE(11,5)|ENVIRONMENT FRIENDLY(11,2)|BIOCHAR BAKING(10,3)|COASTAL SMOOTH BEACH(10,3)|DESTRUCTIVE SAMPLING ASSAY(10,3)|SPARTINA ALTERNIFLORA SOIL CONDITIONER(10,3)|CRUSHER(10,2)|GROUND LAYER(10,2)|COASTAL WETLAND SOIL SALINIZATION(10,1)|CHARCOAL SOIL RATIO(9,5)|CRUCIBLE(9,5)|TINFOIL(9,5)|BAKED BIOCHAR(9,3)|CARBON STORAGE CAPACITY(8,1)|MICROBIAL POPULATION ABUNDANCE(8,1)|WASTE SPARTINA ALTERNIFLORA STRAW(8,1)|SOIL BAG(7,6)|EXPERIMENTAL SOIL(7,4)|ENHANCEMENT MODIFIER(7,3)|DRYING SPARTINA ALTERNIFLORA STRAW(7,1)|ORGANIC CARBON(7,1)|SOIL HYDROLYTIC PROTEASE(7,1)|SOIL MICROBIAL ABUNDANCE(7,1)|SPARTINA ALTERNIFLORA WETLAND(7,1)|ORGANIC CARBON CONTENT(6,4)|PLANT RESIDUE(6,3)|SOIL SAMPLE(6,3)|IMPROVING AGENT(6,2)|BIOMASS CHARCOAL INFLUENCE(6,1)|MANGROVE WETLAND(6,1)|MICROBIAL RICHNESS DECREASE(6,1)|NUTRIENT ION ADSORPTION(6,1)|PHOTOSYNTHETIC BACTERIA(6,1)|SALT BIOGAS DISCOMFORT(6,1)|SPARTINA ALTERNIFLORA BIOCHAR(6,1)|WETLAND ECOSYSTEM ENVIRONMENT MATRIX(6,1)|SUCRASE(5,5)|DETECTION INDEX(5,3)|FINE ROOT(5,3)|MIXING BIOMASS(5,3)|PLANT POWDER(5,3)|SOIL MIX(5,3)|COASTAL WETLAND SOIL CARBON(5,2)|CULTURE EXPERIMENT(5,2)|ABUNDANT DOOR(5,1)|AEROBIC NONOXYGEN(5,1)|BIOCHAR PORE(5,1)|DROUGHT SOIL ECOLOGICAL CHANGE(5,1)|FRAGILE SOIL(5,1)|MODIFYING HEAVY SALINE SOIL(5,1)|SALINE SOIL PLANT(5,1)|SOIL FERTILIZER PRESERVING CAPACITY(5,1)|SOIL PROTEASE(5,1)|SPARTINA ALTERNIFLORA TREATMENT PROJECT(5,1)|100 MESH SIEVE(4,5)|CONSTANT WEIGHT(4,5)|UREASE(4,5)|ALKALINE PHOSPHATASE(4,4)|CARBON RESERVOIR(4,2)|PREPARED BIOCHAR PYROLYSIS TEMPERATURE(4,2)|AVAILABLE RAW MATERIAL(4,1)|BIOMASS CHARCOAL FIRING TEMPERATURE(4,1)|COASTAL SALT MARSH WETLAND(4,1)|DOMINANT BACTERIUM(4,1)|MICROBIAL BIOMASS CARBON CONTENT(4,1)|RAW MATERIAL(4,1)|SALT MARSH PLANT UTILIZATION(4,1)|SOIL MICROORGANISM(4,1)|SOIL SALINITY(4,1)|HIGH TEMPERATURE PYROLYSIS TREATMENT(3,7)|COMPACTION(3,3)|LABORATORY(3,3)|MATURITY PERIOD(3,3)|MUFFLE FURNACE(3,3)|PLASTIC CAP(3,3)|PLASTIC TANK(3,3)|PULVERIZER(3,3)|SCISSORS(3,3)|HEAVY SALTY AREA(3,2)|PROTEUS(3,2)|SIGNIFICANCE(3,2)|SOIL MICROBIAL COMMUNITY STRUCTURE(3,2)|SOIL NUTRIENT(3,2)|ADDING SPARTINA ALTERNIFLORA(3,1)|ALKALINE OXYGEN(3,1)|CARBON DECOMPOSITION(3,1)|CARBON METABOLISM(3,1)|DESERTIFICATION(3,1)|ECOLOGY(3,1)|ENVIRONMENT FRIENDLY SOIL CONDITIONER(3,1)|FLUSHING(3,1)|FTIR SPECTRUM(3,1)|H3A TREATMENT(3,1)|HEAVY SALINITY SOIL(3,1)|MODIFIER TREATMENT(3,1)|OXYGEN ACID(3,1)|REED BIOMASS CHARCOAL ADDITION(3,1)|SALT BIOGAS PLANT GROWTH(3,1)|SALT MARSH LAND(3,1)|SOIL ECOLOGICAL FUNCTION(3,1)|SOIL ENZYMATIC ACTIVITY(3,1)|SOIL OXYGEN CONTENT(3,1)| (CN119929773)|1. The preparation method of the carbon sequestration and sink enhancement and modifier for the heavy salty soil is characterized by comprising the following steps of:| collecting spartina alterniflora straw, crushing, carrying out high-temperature pyrolysis treatment at 350-550 ℃ for 40-80min, and cooling to obtain spartina alterniflora biomass charcoal, namely the heavy saline soil carbon fixation and sequestration and modifier. |2. The preparation method of the carbon sequestration and sequestration enhancement and modification agent for heavy salty soil according to claim 1 is characterized in that before the spartina alterniflora straw is crushed, the spartina alterniflora straw is firstly dried to constant weight, the spartina alterniflora straw is crushed by a crusher and is screened by a 100-mesh sieve (0.149 mm) for later use, and during the high-temperature pyrolysis treatment, the spartina alterniflora straw powder is tightly wrapped by using tinfoil and is subjected to high-temperature pyrolysis in a crucible.|3. The carbon-fixing and sink-increasing and modifying agent for heavy salty soil is characterized in that the carbon-fixing and sink-increasing and modifying agent for heavy salty soil is spartina alterniflora biomass charcoal prepared by the preparation method of claim 1 or 2.|4. The use of the carbon sequestration and sequestration improving agent for heavy salty soil according to claim 3 for improving heavy salty soil.|5. The use according to claim 4, wherein said modifying the heavy salty soil comprises modifying the physicochemical properties, nutrient content and microbial community structure thereof.|6. The use according to claim 4, wherein the improvement of the heavy salty soil comprises an improvement of the carbon fixation effect of the salty plants and the heavy salty soil, and an improvement of the organic carbon content.|7. The use according to claim 6, wherein the salt-biogas plant comprises one or more of spartina alterniflora (Spartina alterniflora), suaeda salsa (Suaeda salsa), reed (PHRAGMITES AUSTRALIS).|8. The method for carbon sequestration and improvement of heavy salted soil is characterized by comprising the step of adopting the agent for carbon sequestration and improvement of heavy salted soil according to claim 3.|9. The method for carbon sequestration and improvement of heavy salty soil according to claim 8, characterized by comprising the following steps:| Spreading the spartina alterniflora biomass charcoal in the heavy saline soil which needs carbon fixation and sink increase according to the charcoal-soil ratio (w: w) of 1 (3-5), and stirring uniformly with the surface soil. |10. The method for carbon sequestration and improvement of heavy salty soil according to claim 9, wherein the superficial soil is a soil layer 0-30cm from the soil surface. (CN119929773)|TECHNICAL FIELD|Technical Field|[0001] The invention discloses a carbon sequestration and sink-increasing and modifying agent for heavy saline soil, a preparation method and application thereof, and belongs to the technical field of ecological environment improvement.|BACKGROUND ART|[0002] The coastal wetland soil carbon reservoir is one of important carbon reservoirs, the carbon reserves of the mangrove wetland can reach 43.49-79.14 t/hm 2, the carbon reserves of the spartina alterniflora wetland can reach 25.50t/hm 2, and the coastal wetland soil carbon reservoir has a quite large lifting space. The salt biogas carbon fixation and sink-increasing technology is a new hot spot direction, and has very important significance on how to utilize vast coastal wetlands to become important carbon sinks and reducing negative ecological effects caused by carbon dioxide emission.|[0003] The wetland soil is used as a main environment matrix of the wetland ecosystem and is a foundation for maintaining and guaranteeing the normal functions of the wetland. However, in the coastal wetland degradation process, salinization, alkalization and desertification often occur in the originally fragile soil, and a large amount of nutrient elements such as carbon, nitrogen, phosphorus and the like in the wetland soil are lost, so that the ecological function of the soil is reduced. Among them, the salinization problem of the coastal wetland soil is most prominent due to the continuous flushing and soaking by seawater for a long time. Currently, a number of physical, chemical and biological measures are used to perform soil remediation and improvement of the heavy saline soil of coastal wetlands. But are limited by cost and application methods, often with limitations in practical use. Therefore, the development of the low-cost and environment-friendly soil conditioner has important significance for the treatment of the heavy saline soil of the coastal wetland.|[0004] The spartina alterniflora is a perennial herb and has the characteristics of extremely wide distribution surface, large biomass and the like. Since being introduced, spartina alterniflora is continuously and rapidly expanded in China as an invasive species. The latest remote sensing image shows that the total occurrence area of the spartina alterniflora reaches 6.8 ten thousand hectares. In order to restore the functions of the wetland and the local ecology, china starts special actions for preventing and controlling spartina alterniflora. Large-scale spartina alterniflora treatment projects were developed from 2019 on all sides. Therefore, the resource utilization of a large amount of spartina alterniflora straw generated by treatment becomes a main problem, and development of an environment-friendly method for realizing the resource utilization of spartina alterniflora is needed.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the technical problems, the invention provides a carbon sequestration and exchange increasing and improving agent for heavy salty soil, and a preparation method and application thereof, which aim to regulate physicochemical properties of soil by preparing and adding the soil improving agent, indirectly change components and structures of organic carbon in the soil by the action of salt marsh plants and salt marsh microorganisms and improve carbon reserves of coastal carbon libraries. Solves the problems of the existing spartina alterniflora straw resource utilization technology and the existing heavy saline soil carbon fixation and sink increasing technology, and the method is efficient and rapid, low in cost and obvious in effect.|[0006] The technical scheme is that in order to achieve the aim of the invention, the invention adopts the following technical scheme:|[0007] The preparation method of the carbon sequestration and sink-increasing and modifying agent for the heavy salty soil comprises the following steps: |[0008] collecting spartina alterniflora straw, crushing, carrying out high-temperature pyrolysis treatment at 350-550 ℃ for 40-80min, and cooling to obtain spartina alterniflora biomass charcoal, namely the heavy saline soil carbon fixation and sequestration and modifier. |[0009] The method comprises the steps of drying spartina alterniflora straw to constant weight before crushing, crushing by a crusher, sieving with a 100-mesh sieve (0.149 mm) for later use, and carrying out high-temperature pyrolysis in a crucible by tightly wrapping spartina alterniflora straw powder by using tinfoil during high-temperature pyrolysis.|[0010] The invention also provides a carbon-fixing and sink-increasing and modifying agent for the heavy-salinity soil, which is spartina alterniflora biomass charcoal prepared by the preparation method.|[0011] The invention also provides application of the heavy saline soil carbon fixation and exchange increase modifier in modifying heavy saline soil.|[0012] As a specific embodiment, the modifying the heavy salty soil comprises altering its physicochemical properties, nutrient content, and microbial community structure.|[0013] As a specific embodiment, the improvement of the heavy salted soil comprises the improvement of the carbon fixation effect of the saline soil plants and the heavy salted soil and the improvement of the organic carbon content.|[0014] Further, the salt marsh plant comprises one or more of spartina alterniflora (Spartina alterniflora), suaeda salsa (Suaeda salsa) and reed (PHRAGMITES AUSTRALIS).|[0015] The invention finally provides a method for carbon fixation, sink enhancement and improvement of heavy saline soil, which comprises the step of adopting the heavy saline soil carbon fixation, sink enhancement and improvement agent to improve the heavy saline soil.|[0016] As a specific embodiment, the method for carbon sequestration, sink enhancement and improvement of heavy saline soil comprises the following steps:|[0017] Spreading the spartina alterniflora biomass charcoal in the heavy saline soil which needs carbon fixation and sink increase according to the charcoal-soil ratio (w: w) of 1 (3-5), and stirring uniformly with the surface soil. |[0018] As a further scheme, the surface soil refers to a soil layer which is 0-30cm from the surface of the soil.|[0019] The invention provides a heavy salty soil carbon fixation and sink enhancement and improving agent and preparation and application thereof, the technical principle is that the waste spartina alterniflora straw is used for preparing soil carbon fixation and exchange improvement agents, and the agents are applied to the coastal wetland heavy salty soil to be improved. Improving physicochemical properties, nutrient conditions, soil hydrolase activity and microbial community structure of the heavy saline soil. After the salt biogas plants growing in the area absorb available nitrogen and phosphorus, the nutrient conditions of the salt biogas plants are changed, the growth is more vigorous, the carbon fixing efficiency of the salt biogas plants can be improved, and the organic carbon content of soil is increased. Meanwhile, the addition of the biochar can also directly improve the total organic carbon content in the soil. After the biochar is added into the soil, a carbon source can be provided for soil microorganisms, so that the activity of the biochar is enhanced. On the other hand, the addition of biochar modifiers also increases the abundance of some functional groups in the soil, such as aerobic non-oxygen producing photosynthetic bacteria that can increase microbial-derived carbon. The activity of dominant bacteria related to carbon metabolism is reduced, so that the carbon decomposition rate of soil is reduced, self-holding of a carbon reservoir is facilitated, and the effects of carbon fixation and sink increase are achieved.|[0020] The carbon fixation and exchange increase and improvement agent for heavy salty soil and the preparation and application thereof can be used in heavy salty soil, mainly aims at heavy salty areas covered by vegetation, and can play a certain role in heavy salty areas not covered by vegetation. Therefore, the application range of the technology is wider, and the technology can be popularized and applied in a large scale.|[0021] The carbon-fixing and sink-increasing modifier for heavy salty soil, provided by the invention, and the preparation and application thereof, have the advantages of simple preparation, easily available raw materials and low cost. The method adopts the invading plant spartina alterniflora straw as a carbon source for supplementing, and is environment-friendly. After the soil carbon fixation and collection increasing and modifying agent is added, the growth of salt biogas plants can be promoted, meanwhile, the soil microbial community structure is changed, and the plant and soil carbon fixation effect can be greatly improved.|[0022] According to the preparation and application technology of the carbon sequestration and sequestration improving agent for the heavy saline soil, the organic carbon sequestration amount of the saline soil can be remarkably improved. Experiments show that the organic carbon content of the soil can be increased by 200% by adding spartina alterniflora charcoal to condition the heavy-salt soil until the end of the experiment.|[0023] Compared with the prior art, the invention provides the carbon sequestration and sequestration improving agent for heavy salty soil, and the preparation method and the application thereof. By implementing the technology, the physicochemical properties of the heavy saline soil are improved, and the nutrient content, the carbon content and the hydrolase activity in the soil are obviously improved. The soil microbial community structure is also greatly changed.|[0024] 1. The invention reasonably and fully utilizes the spartina alterniflora straw to recycle resources, saves the cost of additional carbon sources, and reduces the discomfort of salt biogas microorganisms on strange carbon sources. Solves the technical problems of carbon fixation and sink increase in an environment-friendly way;|[0025] 2. the application method of the soil carbon sequestration and sequestration improving agent provided by the invention has a wide application range, and can be widely applied to carbon sequestration of heavy saline soil; |[0026] 3. the soil carbon fixation and exchange increasing and modifier adding mode provided by the invention can improve the utilization efficiency of the salt-marsh plant on useful components in the modifier, and can also effectively and uniformly distribute the modifier into the salt-marsh soil, thereby improving the treatment efficiency of the modifier. |DRAWINGS DESCRIPTION|[0027] FIG. 1 is a diagram of a process for preparing spartina alterniflora biomass charcoal.|[0028] FIG. 2 is a FTIR spectrum of spartina alterniflora biochar prepared at different firing temperatures.|[0029] FIG. 3 shows the change in soil hydrolase activity after the addition of the soil carbon sequestration and sequestration improving agent.|[0030] Fig. 4 shows the microbial community structure of soil after carbon sequestration and modifier addition.|[0031] FIG. 5 shows the bacterial colony OTUs of soil after carbon sequestration and modifier addition.|INVENTION MODE|Detailed Description|[0032] The invention is further illustrated below with reference to examples.|[0033] Example 1:|[0034] (1) Preparation of experimental soil, namely randomly selecting sampling points from coastal smooth beaches, taking soil bags of 0-20cm by using earth drills, and taking the soil bags back to a laboratory. The fine roots and other plant residues (> 2 mm) in the sampled soil were manually removed. The soil was passed through a 2mm sieve, thoroughly homogenized and air dried. The soil was activated at 25 ℃ with a maximum water holding capacity of 60%, and the soil was weighed every 1d during activation and pre-incubated for 14 days. |[0035] (2) The preparation of the soil carbon fixation and exchange enhancement modifier comprises the steps of harvesting and washing the aerial parts of spartina alterniflora in a mature period, and drying to constant weight at 60 ℃. Then, the mixture was cut into small pieces by scissors, pulverized by a pulverizer, and sieved by a 100-mesh sieve (0.149 mm) for later use. The plant powder is put into a crucible for compaction, tightly wrapped by tinfoil, and put into a muffle furnace for high-temperature pyrolysis treatment, wherein the pyrolysis temperature is 350 ℃ and the treatment time is 1 hour. And after the baking of the biochar is finished, discharging the baked biochar, and cooling to below 60 ℃ at room temperature.|[0036] (3) Uniformly mixing biomass charcoal with soil according to a charcoal-soil ratio (w: w) of 1 (3-5), placing the mixed soil into a 200ml plastic tank, and regulating the water content of the soil to enable the water content of the soil to reach 60% of the maximum water holding capacity. Ventilation and reduced moisture loss throughout the incubation process was achieved by assembly using perforated plastic caps (3 mm per well, 9 wells total). Meanwhile, the water content of the soil is kept unchanged by weighing and adding deionized water. Culturing at 25deg.C under constant temperature and humidity for 30 weeks.|[0037] (4) Destructive sampling assays were performed at 180d,360 d. The detection indexes comprise physical indexes (mechanical composition, volume weight and water content) of soil, chemical indexes (pH, water-soluble salt content and total organic carbon content), biological indexes (soil hydrolase activity (sucrase, urease, alkaline phosphatase and protease) and soil microbial community structure), so as to calculate soil improvement and carbon fixation and sink increase effects.|[0038] Example 2:|[0039] (1) Preparation of experimental soil, namely randomly selecting sampling points from coastal smooth beaches, taking soil bags of 0-20cm by using earth drills, and taking the soil bags back to a laboratory. The fine roots and other plant residues (> 2 mm) in the sampled soil were manually removed. The soil was passed through a 2mm sieve, thoroughly homogenized and air dried. The soil was activated at 25 ℃ with a maximum water holding capacity of 60%, and the soil was weighed every 1d during activation and pre-incubated for 14 days. |[0040] (2) The preparation of the soil carbon fixation and exchange enhancement modifier comprises the steps of harvesting and washing the aerial parts of spartina alterniflora in a mature period, and drying to constant weight at 60 ℃. Then, the mixture was cut into small pieces by scissors, pulverized by a pulverizer, and sieved by a 100-mesh sieve (0.149 mm) for later use. The plant powder is put into a crucible for compaction, tightly wrapped by tinfoil, and put into a muffle furnace for high-temperature pyrolysis treatment, wherein the pyrolysis temperature is 450 ℃ and the treatment time is 1 hour. And after the baking of the biochar is finished, discharging the baked biochar, and cooling to below 60 ℃ at room temperature.|[0041] (3) Uniformly mixing biomass charcoal with soil according to a charcoal-soil ratio (w: w) of 1 (3-5), placing the mixed soil into a 200ml plastic tank, and regulating the water content of the soil to enable the water content to reach 60% of the maximum water holding capacity. Ventilation and reduced moisture loss throughout the incubation process was achieved by assembly using perforated plastic caps (3 mm per well, 9 wells total). Meanwhile, the water content of the soil is kept unchanged by weighing and adding deionized water. Culturing at 25deg.C under constant temperature and humidity for 30 weeks.|[0042] (4) Destructive sampling assays were performed at 180d,360 d. The detection indexes comprise physical indexes (mechanical composition, volume weight and water content) of soil, chemical indexes (pH, water-soluble salt content and total organic carbon content), biological indexes (soil hydrolase activity (sucrase, urease, alkaline phosphatase and protease) and soil microbial community structure), so as to calculate soil improvement and carbon fixation and sink increase effects.|[0043] Example 3:|[0044] (1) Preparation of experimental soil, namely randomly selecting sampling points from coastal smooth beaches, taking soil bags of 0-20cm by using earth drills, and taking the soil bags back to a laboratory. The fine roots and other plant residues (> 2 mm) in the sampled soil were manually removed. The soil was passed through a 2mm sieve, thoroughly homogenized and air dried. The soil was activated at 25 ℃ with a maximum water holding capacity of 60%, and the soil was weighed every 1d during activation and pre-incubated for 14 days. |[0045] (2) The preparation of the soil carbon fixation and exchange enhancement modifier comprises the steps of harvesting and washing the aerial parts of spartina alterniflora in a mature period, and drying to constant weight at 60 ℃. Then, the mixture was cut into small pieces by scissors, pulverized by a pulverizer, and sieved by a 100-mesh sieve (0.149 mm) for later use. The plant powder is put into a crucible for compaction, tightly wrapped by tinfoil, and put into a muffle furnace for high-temperature pyrolysis treatment, wherein the pyrolysis temperature is 550 ℃ and the treatment time is 1 hour. And after the baking of the biochar is finished, discharging the baked biochar, and cooling to below 60 ℃ at room temperature.|[0046] (3) Uniformly mixing biomass charcoal with soil according to a charcoal-soil ratio (w: w) of 1 (3-5), placing the mixed soil into a 200ml plastic tank, and regulating the water content of the soil to enable the water content to reach 60% of the maximum water holding capacity. Ventilation and reduced moisture loss throughout the incubation process was achieved by assembly using perforated plastic caps (3 mm per well, 9 wells total). Meanwhile, the water content of the soil is kept unchanged by weighing and adding deionized water. Culturing at 25deg.C under constant temperature and humidity for 30 weeks.|[0047] (4) Destructive sampling assays were performed at 180d,360 d. The detection indexes comprise physical indexes (mechanical composition, volume weight and water content) of soil, chemical indexes (pH, water-soluble salt content and total organic carbon content) and biological indexes (soil hydrolase activity (sucrase, urease, alkaline phosphatase and protease) and microbial community structure), so that the soil improvement and carbon fixation and sink increase effects are calculated.|[0048] As shown in figure 2, the surface of the biomass charcoal prepared from spartina alterniflora contains more oxygen-containing functional groups such as-OH free radicals, -C=O, -C-O/-C-O-C. The acidic or alkaline oxygen-containing functional groups are beneficial to improving the buffer capacity of soil, enhancing the adsorption of nutrient ions and organic substances and improving the fertilizer-preserving capacity of soil. With the rising of the pyrolysis temperature, the characteristic peak of part of oxygen-containing functional groups gradually disappears, which represents the rising of the condensation degree of carbon chains of the substance carbon in the pyrolysis process, and some oxygen-containing functional groups are broken, crosslinked and cyclized, become aromatic, and the stability is enhanced, which means that the carbon fixation potential of the biomass carbon is increased.|[0049] After the soil conditioner is applied, the nutrient content in the soil is obviously improved. The total nitrogen content was increased by 0.07% and the total phosphorus content was increased by 0.26% (table 1). The improvement of soil nutrients can promote plant growth and reduce the carbon loss of the coastal salt marsh wetland.|[0050] After the soil conditioner is applied, the total carbon and microbial biomass carbon content in the soil is obviously improved. The total carbon content was increased by 1.99% and the microbial biomass carbon was increased by 1.76% (table 2). This shows that the addition of the soil conditioner can directly increase the total organic carbon content in the soil and supplement the carbon source required by the microbial activity.|[0051] Table 1 nutrient lifting effects achieved in the examples|[0052] |[0053] Table 2 soil carbon lifting effect obtained in examples|[0054] |[0055] |[0056] At the end of the culture experiment, the activity of the soil hydrolytic protease was measured, and the measurement results are shown in FIG. three. Wherein A, B, C corresponds to the addition ratio of the soil additive to 1:3, 1:4 and 1:5, and H3, H4, H5 and H6 correspond to the pyrolysis temperatures of the prepared biochar in the soil conditioner to be 300 ℃, 400 ℃, 500 ℃ and 600 ℃. The results of the soil enzyme activity assay showed (FIG. 3) that all soil conditioner addition treatments increased protease, phosphatase, urease and sucrase activity in the soil compared to the no addition treatment group. Compared with the non-additive treatment group, the protease activity of the soil with the spartina alterniflora soil conditioner is obviously increased by 41.46-132.91 percent (P < 0.05), the alkaline phosphatase activity is obviously increased by 30.66-172.76 percent (P < 0.05), the urease activity is obviously increased by 4.40-332.10 percent (P < 0.05), and the sucrase activity is obviously increased by 6.04-179.91 percent (P < 0.05). The soil enzyme activity participates in various soil functional processes and can be used as an index of soil ecological change of drought and semiarid ecological systems. The spartina alterniflora soil conditioner can improve soil nutrient, moisture and ventilation conditions and promote enzymatic reaction. Meanwhile, the biochar pores in the spartina alterniflora soil conditioner can enable oxygen to be dissolved in pore water, so that the oxygen content of soil is increased, and the enzyme activity is improved. However, the influence of biomass charcoal on the activity of soil enzymes is influenced by the firing temperature of the biomass charcoal, the material of the biomass charcoal and the addition amount of the biomass charcoal. In this experiment, all treatment groups significantly improved soil enzyme activity. The biomass charcoal prepared by pyrolysis at 400-600 ℃ has more remarkable effect of improving the enzymatic activity of soil.|[0057] At the end of the culture experiment, the changes in the abundance of the microbial population at the gate level in the experimental soil were measured and analyzed using Illumina HiSeq high throughput sequencing technology. Wherein A, B, C corresponds to the addition ratio of the soil additive to 1:3, 1:4 and 1:5, and H3, H4, H5 and H6 correspond to the pyrolysis temperatures of the prepared biochar in the soil conditioner to be 300 ℃, 400 ℃, 500 ℃ and 600 ℃. The measurement results showed (fig. 4, 5) that the total OUT was mainly of 11 gates 713. Among the relatively abundant doors are Proteus (Proteus), thick-walled (Firmicutes), actinomyces (Actinobacteria), bacteroides (Bacteroidetes) and Curvularia (Chloroflexi). All add processes share 713 OTUs. Except for the H3A treatment, all treatment-specific OTUs were lower in number than the CK treatment group. The quantity of the special OTU in the soil after the addition of the biomass charcoal prepared by using spartina alterniflora as a material is larger than that of the soil after the addition of the reed biomass charcoal. Overall, the biochar added reduces the microbial abundance of the soil. The degree of the decrease of the microbial richness of the soil after the addition gradually increases along with the increase of the pyrolysis temperature of the biochar.|[0058] The specific embodiments set forth above are merely illustrative of the invention and are not intended to be limiting. All other embodiments, which can be obtained by a person skilled in the art without making any inventive effort, are in principle within the scope of protection of the invention. (CN119929773)|TECHNICAL FIELD|Technical Field|[0001] The invention discloses a carbon sequestration and sink-increasing and modifying agent for heavy saline soil, a preparation method and application thereof, and belongs to the technical field of ecological environment improvement.|BACKGROUND ART|[0002] The coastal wetland soil carbon reservoir is one of important carbon reservoirs, the carbon reserves of the mangrove wetland can reach 43.49-79.14 t/hm 2, the carbon reserves of the spartina alterniflora wetland can reach 25.50t/hm 2, and the coastal wetland soil carbon reservoir has a quite large lifting space. The salt biogas carbon fixation and sink-increasing technology is a new hot spot direction, and has very important significance on how to utilize vast coastal wetlands to become important carbon sinks and reducing negative ecological effects caused by carbon dioxide emission.|[0003] The wetland soil is used as a main environment matrix of the wetland ecosystem and is a foundation for maintaining and guaranteeing the normal functions of the wetland. However, in the coastal wetland degradation process, salinization, alkalization and desertification often occur in the originally fragile soil, and a large amount of nutrient elements such as carbon, nitrogen, phosphorus and the like in the wetland soil are lost, so that the ecological function of the soil is reduced. Among them, the salinization problem of the coastal wetland soil is most prominent due to the continuous flushing and soaking by seawater for a long time. Currently, a number of physical, chemical and biological measures are used to perform soil remediation and improvement of the heavy saline soil of coastal wetlands. But are limited by cost and application methods, often with limitations in practical use. Therefore, the development of the low-cost and environment-friendly soil conditioner has important significance for the treatment of the heavy saline soil of the coastal wetland.|[0004] The spartina alterniflora is a perennial herb and has the characteristics of extremely wide distribution surface, large biomass and the like. Since being introduced, spartina alterniflora is continuously and rapidly expanded in China as an invasive species. The latest remote sensing image shows that the total occurrence area of the spartina alterniflora reaches 6.8 ten thousand hectares. In order to restore the functions of the wetland and the local ecology, china starts special actions for preventing and controlling spartina alterniflora. Large-scale spartina alterniflora treatment projects were developed from 2019 on all sides. Therefore, the resource utilization of a large amount of spartina alterniflora straw generated by treatment becomes a main problem, and development of an environment-friendly method for realizing the resource utilization of spartina alterniflora is needed.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the technical problems, the invention provides a carbon sequestration and exchange increasing and improving agent for heavy salty soil, and a preparation method and application thereof, which aim to regulate physicochemical properties of soil by preparing and adding the soil improving agent, indirectly change components and structures of organic carbon in the soil by the action of salt marsh plants and salt marsh microorganisms and improve carbon reserves of coastal carbon libraries. Solves the problems of the existing spartina alterniflora straw resource utilization technology and the existing heavy saline soil carbon fixation and sink increasing technology, and the method is efficient and rapid, low in cost and obvious in effect.|[0006] The technical scheme is that in order to achieve the aim of the invention, the invention adopts the following technical scheme:|[0007] The preparation method of the carbon sequestration and sink-increasing and modifying agent for the heavy salty soil comprises the following steps: |[0008] collecting spartina alterniflora straw, crushing, carrying out high-temperature pyrolysis treatment at 350-550 ℃ for 40-80min, and cooling to obtain spartina alterniflora biomass charcoal, namely the heavy saline soil carbon fixation and sequestration and modifier. |[0009] The method comprises the steps of drying spartina alterniflora straw to constant weight before crushing, crushing by a crusher, sieving with a 100-mesh sieve (0.149 mm) for later use, and carrying out high-temperature pyrolysis in a crucible by tightly wrapping spartina alterniflora straw powder by using tinfoil during high-temperature pyrolysis.|[0010] The invention also provides a carbon-fixing and sink-increasing and modifying agent for the heavy-salinity soil, which is spartina alterniflora biomass charcoal prepared by the preparation method.|[0011] The invention also provides application of the heavy saline soil carbon fixation and exchange increase modifier in modifying heavy saline soil.|[0012] As a specific embodiment, the modifying the heavy salty soil comprises altering its physicochemical properties, nutrient content, and microbial community structure.|[0013] As a specific embodiment, the improvement of the heavy salted soil comprises the improvement of the carbon fixation effect of the saline soil plants and the heavy salted soil and the improvement of the organic carbon content.|[0014] Further, the salt marsh plant comprises one or more of spartina alterniflora (Spartina alterniflora), suaeda salsa (Suaeda salsa) and reed (PHRAGMITES AUSTRALIS).|[0015] The invention finally provides a method for carbon fixation, sink enhancement and improvement of heavy saline soil, which comprises the step of adopting the heavy saline soil carbon fixation, sink enhancement and improvement agent to improve the heavy saline soil.|[0016] As a specific embodiment, the method for carbon sequestration, sink enhancement and improvement of heavy saline soil comprises the following steps:|[0017] Spreading the spartina alterniflora biomass charcoal in the heavy saline soil which needs carbon fixation and sink increase according to the charcoal-soil ratio (w: w) of 1 (3-5), and stirring uniformly with the surface soil. |[0018] As a further scheme, the surface soil refers to a soil layer which is 0-30cm from the surface of the soil.|[0019] The invention provides a heavy salty soil carbon fixation and sink enhancement and improving agent and preparation and application thereof, the technical principle is that the waste spartina alterniflora straw is used for preparing soil carbon fixation and exchange improvement agents, and the agents are applied to the coastal wetland heavy salty soil to be improved. Improving physicochemical properties, nutrient conditions, soil hydrolase activity and microbial community structure of the heavy saline soil. After the salt biogas plants growing in the area absorb available nitrogen and phosphorus, the nutrient conditions of the salt biogas plants are changed, the growth is more vigorous, the carbon fixing efficiency of the salt biogas plants can be improved, and the organic carbon content of soil is increased. Meanwhile, the addition of the biochar can also directly improve the total organic carbon content in the soil. After the biochar is added into the soil, a carbon source can be provided for soil microorganisms, so that the activity of the biochar is enhanced. On the other hand, the addition of biochar modifiers also increases the abundance of some functional groups in the soil, such as aerobic non-oxygen producing photosynthetic bacteria that can increase microbial-derived carbon. The activity of dominant bacteria related to carbon metabolism is reduced, so that the carbon decomposition rate of soil is reduced, self-holding of a carbon reservoir is facilitated, and the effects of carbon fixation and sink increase are achieved.|[0020] The carbon fixation and exchange increase and improvement agent for heavy salty soil and the preparation and application thereof can be used in heavy salty soil, mainly aims at heavy salty areas covered by vegetation, and can play a certain role in heavy salty areas not covered by vegetation. Therefore, the application range of the technology is wider, and the technology can be popularized and applied in a large scale.|[0021] The carbon-fixing and sink-increasing modifier for heavy salty soil, provided by the invention, and the preparation and application thereof, have the advantages of simple preparation, easily available raw materials and low cost. The method adopts the invading plant spartina alterniflora straw as a carbon source for supplementing, and is environment-friendly. After the soil carbon fixation and collection increasing and modifying agent is added, the growth of salt biogas plants can be promoted, meanwhile, the soil microbial community structure is changed, and the plant and soil carbon fixation effect can be greatly improved.|[0022] According to the preparation and application technology of the carbon sequestration and sequestration improving agent for the heavy saline soil, the organic carbon sequestration amount of the saline soil can be remarkably improved. Experiments show that the organic carbon content of the soil can be increased by 200% by adding spartina alterniflora charcoal to condition the heavy-salt soil until the end of the experiment.|[0023] Compared with the prior art, the invention provides the carbon sequestration and sequestration improving agent for heavy salty soil, and the preparation method and the application thereof. By implementing the technology, the physicochemical properties of the heavy saline soil are improved, and the nutrient content, the carbon content and the hydrolase activity in the soil are obviously improved. The soil microbial community structure is also greatly changed.|[0024] 1. The invention reasonably and fully utilizes the spartina alterniflora straw to recycle resources, saves the cost of additional carbon sources, and reduces the discomfort of salt biogas microorganisms on strange carbon sources. Solves the technical problems of carbon fixation and sink increase in an environment-friendly way;|[0025] 2. the application method of the soil carbon sequestration and sequestration improving agent provided by the invention has a wide application range, and can be widely applied to carbon sequestration of heavy saline soil; |[0026] 3. the soil carbon fixation and exchange increasing and modifier adding mode provided by the invention can improve the utilization efficiency of the salt-marsh plant on useful components in the modifier, and can also effectively and uniformly distribute the modifier into the salt-marsh soil, thereby improving the treatment efficiency of the modifier. |DRAWINGS DESCRIPTION|[0027] FIG. 1 is a diagram of a process for preparing spartina alterniflora biomass charcoal.|[0028] FIG. 2 is a FTIR spectrum of spartina alterniflora biochar prepared at different firing temperatures.|[0029] FIG. 3 shows the change in soil hydrolase activity after the addition of the soil carbon sequestration and sequestration improving agent.|[0030] Fig. 4 shows the microbial community structure of soil after carbon sequestration and modifier addition.|[0031] FIG. 5 shows the bacterial colony OTUs of soil after carbon sequestration and modifier addition.|INVENTION MODE|Detailed Description|[0032] The invention is further illustrated below with reference to examples.|[0033] Example 1:|[0034] (1) Preparation of experimental soil, namely randomly selecting sampling points from coastal smooth beaches, taking soil bags of 0-20cm by using earth drills, and taking the soil bags back to a laboratory. The fine roots and other plant residues (> 2 mm) in the sampled soil were manually removed. The soil was passed through a 2mm sieve, thoroughly homogenized and air dried. The soil was activated at 25 ℃ with a maximum water holding capacity of 60%, and the soil was weighed every 1d during activation and pre-incubated for 14 days. |[0035] (2) The preparation of the soil carbon fixation and exchange enhancement modifier comprises the steps of harvesting and washing the aerial parts of spartina alterniflora in a mature period, and drying to constant weight at 60 ℃. Then, the mixture was cut into small pieces by scissors, pulverized by a pulverizer, and sieved by a 100-mesh sieve (0.149 mm) for later use. The plant powder is put into a crucible for compaction, tightly wrapped by tinfoil, and put into a muffle furnace for high-temperature pyrolysis treatment, wherein the pyrolysis temperature is 350 ℃ and the treatment time is 1 hour. And after the baking of the biochar is finished, discharging the baked biochar, and cooling to below 60 ℃ at room temperature.|[0036] (3) Uniformly mixing biomass charcoal with soil according to a charcoal-soil ratio (w: w) of 1 (3-5), placing the mixed soil into a 200ml plastic tank, and regulating the water content of the soil to enable the water content of the soil to reach 60% of the maximum water holding capacity. Ventilation and reduced moisture loss throughout the incubation process was achieved by assembly using perforated plastic caps (3 mm per well, 9 wells total). Meanwhile, the water content of the soil is kept unchanged by weighing and adding deionized water. Culturing at 25deg.C under constant temperature and humidity for 30 weeks.|[0037] (4) Destructive sampling assays were performed at 180d,360 d. The detection indexes comprise physical indexes (mechanical composition, volume weight and water content) of soil, chemical indexes (pH, water-soluble salt content and total organic carbon content), biological indexes (soil hydrolase activity (sucrase, urease, alkaline phosphatase and protease) and soil microbial community structure), so as to calculate soil improvement and carbon fixation and sink increase effects.|[0038] Example 2:|[0039] (1) Preparation of experimental soil, namely randomly selecting sampling points from coastal smooth beaches, taking soil bags of 0-20cm by using earth drills, and taking the soil bags back to a laboratory. The fine roots and other plant residues (> 2 mm) in the sampled soil were manually removed. The soil was passed through a 2mm sieve, thoroughly homogenized and air dried. The soil was activated at 25 ℃ with a maximum water holding capacity of 60%, and the soil was weighed every 1d during activation and pre-incubated for 14 days. |[0040] (2) The preparation of the soil carbon fixation and exchange enhancement modifier comprises the steps of harvesting and washing the aerial parts of spartina alterniflora in a mature period, and drying to constant weight at 60 ℃. Then, the mixture was cut into small pieces by scissors, pulverized by a pulverizer, and sieved by a 100-mesh sieve (0.149 mm) for later use. The plant powder is put into a crucible for compaction, tightly wrapped by tinfoil, and put into a muffle furnace for high-temperature pyrolysis treatment, wherein the pyrolysis temperature is 450 ℃ and the treatment time is 1 hour. And after the baking of the biochar is finished, discharging the baked biochar, and cooling to below 60 ℃ at room temperature.|[0041] (3) Uniformly mixing biomass charcoal with soil according to a charcoal-soil ratio (w: w) of 1 (3-5), placing the mixed soil into a 200ml plastic tank, and regulating the water content of the soil to enable the water content to reach 60% of the maximum water holding capacity. Ventilation and reduced moisture loss throughout the incubation process was achieved by assembly using perforated plastic caps (3 mm per well, 9 wells total). Meanwhile, the water content of the soil is kept unchanged by weighing and adding deionized water. Culturing at 25deg.C under constant temperature and humidity for 30 weeks.|[0042] (4) Destructive sampling assays were performed at 180d,360 d. The detection indexes comprise physical indexes (mechanical composition, volume weight and water content) of soil, chemical indexes (pH, water-soluble salt content and total organic carbon content), biological indexes (soil hydrolase activity (sucrase, urease, alkaline phosphatase and protease) and soil microbial community structure), so as to calculate soil improvement and carbon fixation and sink increase effects.|[0043] Example 3:|[0044] (1) Preparation of experimental soil, namely randomly selecting sampling points from coastal smooth beaches, taking soil bags of 0-20cm by using earth drills, and taking the soil bags back to a laboratory. The fine roots and other plant residues (> 2 mm) in the sampled soil were manually removed. The soil was passed through a 2mm sieve, thoroughly homogenized and air dried. The soil was activated at 25 ℃ with a maximum water holding capacity of 60%, and the soil was weighed every 1d during activation and pre-incubated for 14 days. |[0045] (2) The preparation of the soil carbon fixation and exchange enhancement modifier comprises the steps of harvesting and washing the aerial parts of spartina alterniflora in a mature period, and drying to constant weight at 60 ℃. Then, the mixture was cut into small pieces by scissors, pulverized by a pulverizer, and sieved by a 100-mesh sieve (0.149 mm) for later use. The plant powder is put into a crucible for compaction, tightly wrapped by tinfoil, and put into a muffle furnace for high-temperature pyrolysis treatment, wherein the pyrolysis temperature is 550 ℃ and the treatment time is 1 hour. And after the baking of the biochar is finished, discharging the baked biochar, and cooling to below 60 ℃ at room temperature.|[0046] (3) Uniformly mixing biomass charcoal with soil according to a charcoal-soil ratio (w: w) of 1 (3-5), placing the mixed soil into a 200ml plastic tank, and regulating the water content of the soil to enable the water content to reach 60% of the maximum water holding capacity. Ventilation and reduced moisture loss throughout the incubation process was achieved by assembly using perforated plastic caps (3 mm per well, 9 wells total). Meanwhile, the water content of the soil is kept unchanged by weighing and adding deionized water. Culturing at 25deg.C under constant temperature and humidity for 30 weeks.|[0047] (4) Destructive sampling assays were performed at 180d,360 d. The detection indexes comprise physical indexes (mechanical composition, volume weight and water content) of soil, chemical indexes (pH, water-soluble salt content and total organic carbon content) and biological indexes (soil hydrolase activity (sucrase, urease, alkaline phosphatase and protease) and microbial community structure), so that the soil improvement and carbon fixation and sink increase effects are calculated.|[0048] As shown in figure 2, the surface of the biomass charcoal prepared from spartina alterniflora contains more oxygen-containing functional groups such as-OH free radicals, -C=O, -C-O/-C-O-C. The acidic or alkaline oxygen-containing functional groups are beneficial to improving the buffer capacity of soil, enhancing the adsorption of nutrient ions and organic substances and improving the fertilizer-preserving capacity of soil. With the rising of the pyrolysis temperature, the characteristic peak of part of oxygen-containing functional groups gradually disappears, which represents the rising of the condensation degree of carbon chains of the substance carbon in the pyrolysis process, and some oxygen-containing functional groups are broken, crosslinked and cyclized, become aromatic, and the stability is enhanced, which means that the carbon fixation potential of the biomass carbon is increased.|[0049] After the soil conditioner is applied, the nutrient content in the soil is obviously improved. The total nitrogen content was increased by 0.07% and the total phosphorus content was increased by 0.26% (table 1). The improvement of soil nutrients can promote plant growth and reduce the carbon loss of the coastal salt marsh wetland.|[0050] After the soil conditioner is applied, the total carbon and microbial biomass carbon content in the soil is obviously improved. The total carbon content was increased by 1.99% and the microbial biomass carbon was increased by 1.76% (table 2). This shows that the addition of the soil conditioner can directly increase the total organic carbon content in the soil and supplement the carbon source required by the microbial activity.|[0051] Table 1 nutrient lifting effects achieved in the examples|[0052] |[0053] Table 2 soil carbon lifting effect obtained in examples|[0054] |[0055] |[0056] At the end of the culture experiment, the activity of the soil hydrolytic protease was measured, and the measurement results are shown in FIG. three. Wherein A, B, C corresponds to the addition ratio of the soil additive to 1:3, 1:4 and 1:5, and H3, H4, H5 and H6 correspond to the pyrolysis temperatures of the prepared biochar in the soil conditioner to be 300 ℃, 400 ℃, 500 ℃ and 600 ℃. The results of the soil enzyme activity assay showed (FIG. 3) that all soil conditioner addition treatments increased protease, phosphatase, urease and sucrase activity in the soil compared to the no addition treatment group. Compared with the non-additive treatment group, the protease activity of the soil with the spartina alterniflora soil conditioner is obviously increased by 41.46-132.91 percent (P < 0.05), the alkaline phosphatase activity is obviously increased by 30.66-172.76 percent (P < 0.05), the urease activity is obviously increased by 4.40-332.10 percent (P < 0.05), and the sucrase activity is obviously increased by 6.04-179.91 percent (P < 0.05). The soil enzyme activity participates in various soil functional processes and can be used as an index of soil ecological change of drought and semiarid ecological systems. The spartina alterniflora soil conditioner can improve soil nutrient, moisture and ventilation conditions and promote enzymatic reaction. Meanwhile, the biochar pores in the spartina alterniflora soil conditioner can enable oxygen to be dissolved in pore water, so that the oxygen content of soil is increased, and the enzyme activity is improved. However, the influence of biomass charcoal on the activity of soil enzymes is influenced by the firing temperature of the biomass charcoal, the material of the biomass charcoal and the addition amount of the biomass charcoal. In this experiment, all treatment groups significantly improved soil enzyme activity. The biomass charcoal prepared by pyrolysis at 400-600 ℃ has more remarkable effect of improving the enzymatic activity of soil.|[0057] At the end of the culture experiment, the changes in the abundance of the microbial population at the gate level in the experimental soil were measured and analyzed using Illumina HiSeq high throughput sequencing technology. Wherein A, B, C corresponds to the addition ratio of the soil additive to 1:3, 1:4 and 1:5, and H3, H4, H5 and H6 correspond to the pyrolysis temperatures of the prepared biochar in the soil conditioner to be 300 ℃, 400 ℃, 500 ℃ and 600 ℃. The measurement results showed (fig. 4, 5) that the total OUT was mainly of 11 gates 713. Among the relatively abundant doors are Proteus (Proteus), thick-walled (Firmicutes), actinomyces (Actinobacteria), bacteroides (Bacteroidetes) and Curvularia (Chloroflexi). All add processes share 713 OTUs. Except for the H3A treatment, all treatment-specific OTUs were lower in number than the CK treatment group. The quantity of the special OTU in the soil after the addition of the biomass charcoal prepared by using spartina alterniflora as a material is larger than that of the soil after the addition of the reed biomass charcoal. Overall, the biochar added reduces the microbial abundance of the soil. The degree of the decrease of the microbial richness of the soil after the addition gradually increases along with the increase of the pyrolysis temperature of the biochar.|[0058] The specific embodiments set forth above are merely illustrative of the invention and are not intended to be limiting. All other embodiments, which can be obtained by a person skilled in the art without making any inventive effort, are in principle within the scope of protection of the invention. Family Number|(114438809)|114438809|Abstract|(CN119929773 A)|The invention discloses a heavy salinized soil carbon sequestration and sink increasing and modifying agent as well as a preparation method and application of the heavy salinized soil carbon sequestration and sink increasing and modifying agent . The preparation method of the heavy salinized soil carbon sequestration and sink increasing and modifying agent comprises the following steps : collecting spartina alterniflora straws , crushing , performing high - temperature pyrolysis treatment for 40-80 minutes under the condition of 350-550 DEG C , and cooling to obtain spartina alterniflora biomass charcoal , namely the heavy salinized soil carbon sequestration and sink increasing and modifying agent . According to the method , the three targets of resource utilization of the waste straw , improvement of the coastal heavy salinized soil and carbon sequestration and carbon sink increase of the coastal heavy salinized wetland are achieved at the same time , the soil carbon reserve of the coastal wetland can be increased , and the carbon storage function of the wetland is greatly enhanced . |IPC codes|(CN119929773 A)|C01B - 032/05 |Title|(CN119929773 A)|Heavy salinized soil carbon sequestration and sink increasing and modifying agent as well as preparation method and application thereof | Basic materials chemistry|Materials, metallurgy C01B-032/05|C09K-017/02 C01B-032/05|C09K-017/02 PENDING (CN119929773)|PENDING ALIVE (CN119929773)|ALIVE (CN119929773)|LEGAL DETAILS FOR CN119929773|Actual or expected expiration date=2045-01-02|Legal state=ALIVE|Status=PENDING|Event publication date=2025-01-02|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510001550|Application date=2025-01-02|Standardized application number=2025CN-0001550|Event publication date=2025-05-06|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119929773|Publication stage code=A|Publication date=2025-05-06|Standardized publication number=CN119929773|Event publication date=2025-05-06|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-05-23|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN119929773)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTaEfDSKQ5hElfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000077397024&ekey=2088&xpn=CN119929773&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=RJ3hvnRaSY9fcRsRUWdEQ5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN119929773)|CN (CN119929773)|NAME=NANJING NORMAL UNIVERSITY , COUNTRY=CN (CN119929773)|NAME=ZHENG LIFA;NANJING ZHONGLV INTELLECTUAL PROPERTY AGENCY FRIM(GENERAL PARTNERSHIP) , REG=32341 (CN119929773)|NAME=LIU JINE|NAME=ZHANG WEITING|NAME=SONG GE|NAME=LUO XIN|NAME=LAI JIANPING|NAME=LIU HANZHONG|NAME=LIN XIAOWEN|NAME=SUN MINNAN 0 1 Titre: (CN119929773)|Heavy salinized soil carbon sequestration and sink increasing and modifying agent as well as preparation method and application thereof Résumé: (CN119929773)|The invention discloses a heavy salinized soil carbon sequestration and sink increasing and modifying agent as well as a preparation method and application of the heavy salinized soil carbon sequestration and sink increasing and modifying agent. The preparation method of the heavy salinized soil carbon sequestration and sink increasing and modifying agent comprises the following steps: collecting spartina alterniflora straws, crushing, performing high-temperature pyrolysis treatment for 40-80 minutes under the condition of 350-550 DEG C, and cooling to obtain spartina alterniflora biomass charcoal, namely the heavy salinized soil carbon sequestration and sink increasing and modifying agent. According to the method, the three targets of resource utilization of the waste straw, improvement of the coastal heavy salinized soil and carbon sequestration and carbon sink increase of the coastal heavy salinized wetland are achieved at the same time, the soil carbon reserve of the coastal wetland can be increased, and the carbon storage function of the wetland is greatly enhanced. 13 Abstract gpt-4o-mini no The focus is on a carbon sequestration agent derived from biomass charcoal, not on accelerating mineral weathering or CO₂ capture through mineral processes.
10 CN202310416466 CN202310416466 CN116272480|CN116272480 105416955 CN116272480 B 2025-07-11 [CN116272480B]|CN116272480 A 2023-06-23 [CN116272480] 2023-04-19 2023-04-19 2025-07-11|2023-06-23 (CN116272480B)|2025-07-11 (CN116272480)|2043-04-19 (CN116272480)|Stirring assembly and carbon fixation wall insulation material production equipment (CN116272480)|The invention relates to the technical field of stirring plates, in particular to a stirring assembly and carbon-sequestration wall thermal insulation material production equipment, which comprises a stirring plate, one end of the stirring plate is provided with a mounting assembly, the surface of the mounting assembly is provided with a locking assembly, the surface of the stirring plate is provided with a crushing assembly, and the crushing assembly is used for crushing caked materials. A material conveying mechanism is arranged at the other end of the stirring plate and disperses and mixes materials at the other end of the stirring plate to the upper side and the lower side; the stirring assembly and the carbon-sequestration wall thermal insulation material production equipment have the beneficial effects that the mounting assembly is adopted to be matched with the locking assembly, so that the stirring plate is detachably mounted on a traditional stirring shaft, and the deformed stirring plate can be independently replaced in the later period; and the material conveying mechanism is additionally arranged on the stirring plate, so that the materials at the horizontal height of the stirring plate are conveyed to the upper side and the lower side, and the material mixing uniformity of the stirring plate is improved. SECOND CONSTRUCTION|SHANDONG BUILDING ENERGY CONSERVATION ASSOCIATION (CN116272480)|THE SECOND CONSTRUCTION CO. LTD. OF CHINA CONSTRUCTION EIGHTH ENGINEERING DIVISION ([CN])|Shandong Building Energy Conservation Association|(CN116272480)|THE SECOND CONSTRUCTION CO. LTD. OF CHINA CONSTRUCTION EIGHTH ENGINEERING DIVISION ([CN])|Shandong Building Energy Conservation Association ZHU RENJIE|LI CHAO|XU BEI|WANG DAWEI|JIA YUDONG (CN116272480)|ZHU RENJIE|LI CHAO|XU BEI|WANG DAWEI|JIA YUDONG|(CN116272480)|ZHU RENJIE|LI CHAO|XU BEI|WANG DAWEI|JIA YUDONG (CN116272480)|JIANG MING;JINAN XINDA PATENT OFFICE CO. LTD.|Reg. Nb: 37100 (CN116272480)|But the equal fixed welding of stirring board on traditional (mixing) shaft surface is on the (mixing) shaft, when the stirring board long-term use appears warping and influences the stirring effect, is inconvenient for changing single stirring board, and when traditional stirring board rotates along with the (mixing) shaft, only can realize stirring board place level's material and mix, is inconvenient for promoting stirring homogeneity.| (CN116272480)|1. The stirring assembly comprises a stirring plate (1) and is characterized in that one end of the stirring plate (1) is provided with a mounting assembly, the surface of the mounting assembly is provided with a locking assembly, the surface of the stirring plate (1) is provided with a crushing assembly for crushing caking materials, the other end of the stirring plate (1) is provided with a material conveying mechanism, and the materials at the other end of the stirring plate (1) are dispersed and mixed at the upper side and the lower side; the installation component comprises a hooping plate (2), an embedding groove (3), a rubber clamping strip (4) and a positioning inserting block (5), wherein the positioning inserting block (5) is fixed on the inner annular surface of the hooping plate (2), the embedding groove (3) is provided with two groups, the two groups of embedding grooves (3) are symmetrically distributed about the positioning inserting block (5), the two groups of embedding grooves (3) are all arranged on the inner annular surface of the hooping plate (2), the rubber clamping strip (4) is fixed in the embedding groove (3), the width of the rubber clamping strip (4) is larger than the depth of the embedding groove (3), the locking component comprises a reserved groove (6), a connecting slot (7), a connecting inserting piece (8), a penetrating opening (9), a stop block (10) and an elastic traction belt (11), the reserved groove (6) is provided with two groups, the two groups of reserved grooves (6) are respectively arranged on the top surfaces of the plate bodies at two ends of the hooping plate (2), the connecting slot (7) is arranged on the bottom surface of the reserved groove (6), the connecting plug-in unit (8) is of a pi-shaped platy structure, the connecting plug-in unit (8) comprises two parallel side plates and top plates fixed on the two groups of side plates, the two parallel side plates of the connecting plug-in unit (8) are movably inserted into the two groups of connecting slots (7) respectively, the top plates of the connecting plug-in unit (8) are lapped on the reserved slots (6), the penetrating holes (9) are formed in the end plate body of the hoop plate (2), the penetrating holes (9) are in one-to-one correspondence with the reserved slots (6), the penetrating holes (9) are communicated with the reserved slots (6), the stop blocks (10) are movably inserted into the penetrating holes (9), and when the top plates of the connecting plug-in unit (8) are lapped on the reserved slots (6), the stop blocks (10) are positioned above the top plates of the connecting plug-in unit (8) to realize anti-falling limit on the connecting plug-in unit (8).| (CN116272480)|The invention aims to provide a stirring assembly and carbon-fixing wall surface heat-insulating material production equipment so as to solve the problems in the background technology.|The invention relates to the technical field of stirring plates, in particular to a stirring assembly and carbon-fixing wall surface heat-insulating material production equipment.|The invention relates to the technical field of stirring plates, in particular to stirring components and carbon-fixing wall surface heat-insulating material production equipment, which comprises a stirring plate, wherein one end of the stirring plate is provided with a mounting component, the surface of the mounting component is provided with a locking component, the surface of the stirring plate is provided with a crushing component for crushing caking materials, the other end of the stirring plate is provided with a material conveying mechanism for dispersing and mixing the materials at the other end of the stirring plate on the upper side and the lower side.| (CN116272480)|EMBEDDING GROOVE(100,10)|PRODUCTION EQUIPMENT(100,6)|CARBON FIXATION(100,4)|WALL INSULATION MATERIAL(100,1)|PENETRATION(80,4)|STIRRING PLATE(72,61)|ELASTIC TRACTION BELT(70,8)|HOOPING PLATE(66,5)|GROOVE RESERVATION(65,17)|PLUGIN(62,18)|SLOT RESERVATION(61,11)|STIRRING HOMOGENEITY PROMOTION(60,1)|STIRRING BOARD(53,3)|BATTERY COMPARTMENT(48,8)|EMBEDDING GROOVE DEPTH(43,2)|RUBBER CLAMPING STRIP(40,7)|BLOCK INSERTION(39,3)|LOCKING COMPONENT(38,2)|ANTIFALLING LIMIT(38,1)|CRUSHING COMPONENT(35,1)|CRUSHING CAKING MATERIAL(33,4)|COMPONENT MOUNTING(32,2)|CRUSHING(28,6)|STIRRING COMPONENT(27,1)|HOOP PLATE(25,7)|SPIRAL CONVEYING SHAFT(22,6)|CARBON FIXING WALL(21,8)|PENETRATING OPENING(21,3)|INSTALLATION COMPONENT(21,2)|RUBBER CLAMPING STRIP WIDTH(21,2)|WARPING(21,1)|PLATY STRUCTURE(19,4)|DISCHARGE PORT(19,1)|SLITTING BLADE CUTTING EDGE(19,1)|STIRRING BOARD PLACE(19,1)|SUPPORT COLUMN(18,10)|MOUNTING GROOVE NOTCH(17,2)|PROTECTIVE COVER(15,14)|WEARING MOUTH(14,6)|CHANGING SINGLE STIRRING BOARD(14,1)|EQUAL FIXED WELDING(14,1)|PI SHAPED PLATY STRUCTURE(14,1)|INNER ANNULAR SURFACE(13,2)|HOOPING PLATE END(13,1)|MIXING(13,1)|STOP BLOCK(12,18)|SPIRAL MATERIAL CONVEYING SHAFT(12,6)|BAFFLE PLATE(12,4)|BATTERY BIN(11,5)|CUTTING KNIFE(11,5)|SEALING PLATE(10,13)|STORAGE BATTERY(10,10)|EMBEDDED GROOVE(10,6)|STIRRING SHAFT(9,7)|DIAMOND CYLINDER STRUCTURE(9,3)|ELASTIC TRACTION CROSSING NODE(9,1)|MOUNTING COMPONENT SURFACE(9,1)|MOUNTING SURFACE(8,3)|SLITTING KNIFE PLATE(7,2)|EPS EXTERIOR INSULATION(7,1)|RESILIENCE TRACTION(7,1)|STRETCH DRAW ELASTICITY TRACTION(7,1)|POWER SUPPLY(6,5)|SHAFT SURFACE(6,2)|LEVEL MATERIAL(6,1)|TOP PLATE(5,12)|EMBEDDING(5,3)|HOOP PLATE END PLATE(5,3)|MATERIAL OUTLET(5,3)|HOOP BOARD(5,2)|UPPER SIDE(4,6)|INNER RING(4,5)|MOUNTING OPENING SURFACE(4,3)|ANTIDROP(4,2)|DISCHARGE HOLE(4,2)|DEFORMED STIRRING PLATE REPLACEMENT(4,1)|MINED OIL(4,1)|ORDINARY SKILL PERSON(4,1)|ROOF OVERLAP JOINT(4,1)|SLITTING KNIFE CUTTING EDGE(4,1)|SURFACE HEAT INSULATION(4,1)|PARALLEL SIDE PLATE(3,4)|CARBON SEQUESTRATION(3,3)|STIRRING PLATE HORIZONTAL HEIGHT(3,3)|EXTERIOR WALL(3,2)|BIOSOLID(3,1)|CARBOHYDRATE(3,1)|CARBON RESERVOIR CARBON CONTENT(3,1)||(CN116272480)|STIRRING BOARD(100,17)|PRODUCTION EQUIPMENT(100,6)|CARBON FIXATION(100,4)|WALL INSULATION MATERIAL(100,2)|STIRRING PLATE(71,53)|RESERVATION GROOVE(68,10)|SLITTING KNIFE BOARD(68,4)|BROKEN SUBASSEMBLY(45,2)|STIRRING SHAFT(43,11)|ELASTIC TRACTION BELT(43,7)|PROTECTION CASING(42,5)|PEG GRAFTING(41,1)|INSTALLATION COMPONENT(40,6)|BATTERY BIN(38,8)|STIRRING SUBASSEMBLY(37,1)|EMBEDDED GROOVE(33,12)|ELASTICITY TRACTION BELT(33,1)|STIRRING UNIFORMITY(33,1)|SPIRAL CONVEYING AXLE(32,1)|DEFORMED STIRRING PLATE(30,3)|HOOP BOARD(29,5)|CRUSHING CAKING MATERIAL(28,2)|INTERCOMMUNICATION(25,2)|SUBASSEMBLY(25,1)|CRUSHING(24,4)|LOCKING SUBASSEMBLY(24,1)|ROOF OVERLAP JOINT(23,3)|STIRRING BOARD MATERIAL(23,3)|CRUSHING COMPONENT(23,1)|COMPONENT MOUNTING(21,2)|HOMOGENEITY(21,1)|STIRRING BOARD SURFACE(20,4)|BUCKLE PLATE(20,2)|GROOVE RESERVATION(19,12)|SPIRAL CONVEYING SHAFT(19,6)|HORIZONTAL HEIGHT(19,5)|MOUNTING OPENING(18,19)|DOG(18,4)|WEAR MOUTH(18,1)|CARBON FIXING WALL(17,8)|LOCKING COMPONENT(17,1)|STIRRING BOARD END(16,3)|LATE PERIOD(16,2)|ROOFTOP(16,1)|SUPPORT COLUMN(14,10)|ANTICREEP(14,1)|WEARING MOUTH(12,6)|INTERIOR ANCHOR RING(12,4)|DRAW MATERIAL PIPE(12,2)|INSTALLATION COMPONENT SURFACE(12,2)|HOOP PLATE(11,6)|BAFFLE PLATE(10,4)|PARALLEL DISTRIBUTION CURB PLATE(10,2)|PROTECTION COVER(10,2)|FONT(10,1)|SLOT RESERVATION(9,7)|LOCATION BLOCK INSERTION(9,6)|BATTERY COMPARTMENT(9,5)|MIXING EQUIPMENT(9,1)|SOLID CARBON(9,1)|SEALING PLATE(8,13)|PLUGIN(8,11)|STORAGE BATTERY(8,10)|OFFER(8,3)|SYMMETRIC DISTRIBUTION(8,2)|MATERIAL GUIDING PIPE(8,1)|MOUNTING SURFACE(8,1)|DIAMOND CYLINDER STRUCTURE(7,3)|PLATY STRUCTURE(7,3)|SLITTING KNIFE PLATE(7,3)|PRODUCTION FACILITY(7,1)|BREAK UP CAKING MATERIAL(6,2)|LEVELING POSITION(6,1)|MOUNTING COMPONENT SURFACE(6,1)|MOUNTING GROOVE POSITION(6,1)|POWER SUPPLY MODULE(6,1)|RESILIENCE TRACTION(6,1)|STRETCH DRAW ELASTICITY TRACTION(6,1)|STOP BLOCK(5,15)|EMBEDDING GROOVE DEPTH(5,1)|INNER RING OPENING(4,1)|MOUNTING OPENING SURFACE(3,3)|ANTIDROP(3,2)|DISCHARGE HOLE(3,2)|CARBON RESERVOIR DIVISION(3,1)|HOOPING PLATE(3,1)|MINED OIL(3,1)|ORDINARY SKILL PERSON(3,1)| (CN116272480)|1. The stirring assembly comprises a stirring plate (1) and is characterized in that one end of the stirring plate (1) is provided with a mounting assembly, the surface of the mounting assembly is provided with a locking assembly, the surface of the stirring plate (1) is provided with a crushing assembly for crushing caking materials, the other end of the stirring plate (1) is provided with a material conveying mechanism, and the materials at the other end of the stirring plate (1) are dispersed and mixed at the upper side and the lower side; the installation component comprises a hooping plate (2), an embedding groove (3), a rubber clamping strip (4) and a positioning inserting block (5), wherein the positioning inserting block (5) is fixed on the inner annular surface of the hooping plate (2), the embedding groove (3) is provided with two groups, the two groups of embedding grooves (3) are symmetrically distributed about the positioning inserting block (5), the two groups of embedding grooves (3) are all arranged on the inner annular surface of the hooping plate (2), the rubber clamping strip (4) is fixed in the embedding groove (3), the width of the rubber clamping strip (4) is larger than the depth of the embedding groove (3), the locking component comprises a reserved groove (6), a connecting slot (7), a connecting inserting piece (8), a penetrating opening (9), a stop block (10) and an elastic traction belt (11), the reserved groove (6) is provided with two groups, the two groups of reserved grooves (6) are respectively arranged on the top surfaces of the plate bodies at two ends of the hooping plate (2), the connecting slot (7) is arranged on the bottom surface of the reserved groove (6), the connecting plug-in unit (8) is of a pi-shaped platy structure, the connecting plug-in unit (8) comprises two parallel side plates and top plates fixed on the two groups of side plates, the two parallel side plates of the connecting plug-in unit (8) are movably inserted into the two groups of connecting slots (7) respectively, the top plates of the connecting plug-in unit (8) are lapped on the reserved slots (6), the penetrating holes (9) are formed in the end plate body of the hoop plate (2), the penetrating holes (9) are in one-to-one correspondence with the reserved slots (6), the penetrating holes (9) are communicated with the reserved slots (6), the stop blocks (10) are movably inserted into the penetrating holes (9), and when the top plates of the connecting plug-in unit (8) are lapped on the reserved slots (6), the stop blocks (10) are positioned above the top plates of the connecting plug-in unit (8) to realize anti-falling limit on the connecting plug-in unit (8).|2. The stirring assembly according to claim 1, wherein an inclined plane is arranged on the top surface of one end of the stop block (10) extending into the reserved groove (6), the center of the other end of the stop block (10) is fixed on a crossing node of the elastic traction belt (11), the elastic traction belt (11) is in a cross-shaped platy structure, and four ends of the elastic traction belt (11) are fixed on the surface of an end plate body of the hoop plate (2).|3. The stirring assembly of claim 1, wherein the crushing assembly comprises mounting openings (12) and slitting blades (13), the mounting openings (12) are formed in the surface of the stirring plate (1), the mounting openings (12) are formed in a plurality, the mounting openings (12) are distributed along the long side of the stirring plate (1), the slitting blades (13) are of a diamond cylinder structure, the slitting blades (13) are fixed on the surface of the mounting openings (12), and the cutting edges of the slitting blades (13) protrude out of the mounting openings (12).|4. The stirring assembly according to claim 1, wherein the material conveying mechanism comprises two groups of mounting grooves (14), a motor (15), a sealing plate (16), a spiral material conveying shaft (17), a protective cover (18), a supporting column (19), a material outlet (20) and a material guiding pipe (21), wherein the mounting grooves (14) are respectively formed in the top surface of the stirring plate (1) and the bottom surface of the stirring plate (1), the motor (15) is fixed in the mounting grooves (14), a shaft body of the motor (15) penetrates through an inner ring opening of the sealing plate (16), the sealing plate (16) is of an annular plate-shaped structure, the sealing plate (16) is fixed at a notch of the mounting grooves (14), and the spiral material conveying shaft (17) is fixed on the shaft body of the motor (15).|5. The stirring assembly of claim 4, wherein the protective cover (18) is sleeved on the outer side of the spiral conveying shaft (17), one end of the protective cover (18) is fixedly provided with a plurality of support columns (19), one end of each support column (19) is fixed on the surface of the stirring plate (1), the discharge port (20) is formed in the surface of the protective cover (18), the material guiding pipe (21) is fixed on the outer wall of the protective cover (18), the material guiding pipe (21) is communicated with the protective cover (18), and the other end of the stirring plate (1) is provided with a power supply assembly for supplying power to the motor (15).|6. The stirring assembly of claim 5, wherein the power supply assembly comprises a battery compartment (22), a storage battery (23) and a baffle plate (24), the battery compartment (22) is arranged at the other end of the stirring plate (1), the storage battery (23) is fixed in the battery compartment (22), the storage battery (23) is connected with the motor (15) through a wire, the baffle plate (24) is fixed at the other end of the stirring plate (1) through a screw, and the baffle plate (24) seals the battery compartment (22).|7. A carbon-fixing wall surface heat insulation material production device is characterized by comprising the stirring assembly as set forth in any one of claims 1-6. (CN116272480)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of stirring plates, in particular to a stirring assembly and carbon-fixing wall surface heat-insulating material production equipment.|BACKGROUND ART|[0002] Carbon sequestration refers to measures to increase the carbon content of a carbon reservoir other than the atmosphere. Including physical carbon fixation and biological carbon fixation. Physical carbon sequestration is the long term storage of carbon dioxide in mined oil and gas wells, coal seams, and deep seas. Biosolids are the conversion of carbon dioxide in the atmosphere, which is inorganic carbon, to organic carbon, which is carbohydrate, and are immobilized in plants or in soil.|[0003] In the prior art, the wall heat-insulating material (also called as inorganic active wall heat-insulating material) can save a large amount of wall materials, improve the heat-insulating performance of the wall, save resources and reduce environmental pollution, is a novel material for heat insulation of inner and outer walls, and can be used for most structures of any building by using the wooden material, thereby achieving the purpose of carbon fixation. The aim of reducing carbon emission is fulfilled. The maximum potential for carbon sequestration can be achieved in exterior walls, floors and roof structures. For example, passive rooms designed for cold climates have two alternate building exterior wall systems, wood frame walls filled with insulation and concrete walls insulated with EPS exterior insulation. When the carbon-fixing wall surface heat-insulating material is produced, the materials are mixed by virtue of a stirring shaft.|[0004] But the equal fixed welding of stirring board on traditional (mixing) shaft surface is on the (mixing) shaft, when the stirring board long-term use appears warping and influences the stirring effect, is inconvenient for changing single stirring board, and when traditional stirring board rotates along with the (mixing) shaft, only can realize stirring board place level's material and mix, is inconvenient for promoting stirring homogeneity.|DISCLOSURE|Disclosure of Invention|[0005] The invention aims to provide a stirring assembly and carbon-fixing wall surface heat-insulating material production equipment so as to solve the problems in the background technology.|[0006] In order to achieve the purpose, the stirring assembly comprises a stirring plate, wherein one end of the stirring plate is provided with a mounting assembly, the surface of the mounting assembly is provided with a locking assembly, the surface of the stirring plate is provided with a crushing assembly for crushing caking materials, the other end of the stirring plate is provided with a material conveying mechanism, and the materials at the other end of the stirring plate are dispersed and mixed on the upper side and the lower side.|[0007] Preferably, the installation component includes hoop board, embedded groove, rubber clip strip and location inserted block, and the location inserted block is fixed on the interior anchor ring of hoop board, and the embedded groove is equipped with two sets of, and two sets of embedded grooves are about the location inserted block symmetric distribution, and two sets of embedded grooves all offer on the interior anchor ring of hoop board, and the rubber clip strip is fixed in the embedded groove, and the width of rubber clip strip is greater than the degree of depth of embedded groove.|[0008] Preferably, the locking assembly comprises two reserved grooves, connecting slots, connecting plug-ins, penetrating openings, stop blocks and elastic traction belts, wherein the two reserved grooves are respectively arranged on the top surfaces of plate bodies at two ends of the hoop plate, the connecting slots are respectively arranged on the bottom surfaces of the reserved grooves, the connecting plug-ins are of a pi-shaped plate structure, the connecting plug-ins comprise two side plates which are distributed in parallel and top plates which are fixed on the two groups of side plates, the two side plates which are distributed in parallel of the connecting plug-ins are respectively movably inserted into the two groups of connecting slots, and the top plates of the connecting plug-ins are lapped on the reserved grooves.|[0009] Preferably, the wearing mouth is arranged on the end plate body of the hooping plate, the wearing mouth corresponds to the reserved groove one by one, the wearing mouth is communicated with the reserved groove, the stop block is movably inserted into the wearing mouth, the stop block penetrates through the wearing mouth and then stretches into the reserved groove, when the top plate of the connecting plug-in unit is lapped on the reserved groove, the stop block is positioned above the top plate of the connecting plug-in unit, and the anti-drop limit of the connecting plug-in unit is realized.|[0010] Preferably, the top surface of one end of the stop block extending into the reserved groove is provided with an inclined plane, the center of the other end of the stop block is fixed on a cross joint of the elastic traction belt, the elastic traction belt is of a cross-shaped platy structure, and four ends of the elastic traction belt are fixed on the surface of an end plate body of the hoop plate.|[0011] Preferably, the crushing assembly comprises a mounting opening and a slitting knife plate, wherein the mounting opening is formed in the surface of the stirring plate, a plurality of mounting openings are formed in the mounting opening, the mounting openings are distributed along the long side of the stirring plate, the slitting knife plate is of a diamond cylinder structure, the slitting knife plate is fixed on the surface of the mounting opening, and the cutting edge of the slitting knife plate protrudes out of the mounting opening.|[0012] Preferably, the conveying mechanism comprises a mounting groove, a motor, a sealing plate, a spiral conveying shaft, a protective cover, a support column, a discharge hole and a material guiding pipe, wherein the mounting groove is provided with two groups, the two groups of mounting grooves are respectively formed in the top surface of the stirring plate and the bottom surface of the stirring plate, the motor is fixed in the mounting groove, a shaft body of the motor penetrates through an inner ring opening of the sealing plate, the sealing plate is of an annular plate-shaped structure, the sealing plate is fixed at a notch of the mounting groove, and the spiral conveying shaft is fixed on the shaft body of the motor.|[0013] Preferably, the protective cover is sleeved on the outer side of the spiral conveying shaft, one end of the protective cover is fixed with a plurality of support columns, one end of each support column is fixed on the surface of the stirring plate, the discharge hole is formed in the surface of the protective cover, the material guiding pipe is fixed on the outer wall of the protective cover, the material guiding pipe is communicated with the protective cover, and the other end of the stirring plate is provided with a power supply assembly for supplying power to the motor.|[0014] Preferably, the power supply assembly comprises a battery compartment, a storage battery and a baffle, wherein the battery compartment is arranged at the other end of the stirring plate, the storage battery is fixed in the battery compartment, the storage battery is connected with the motor through a wire, the baffle is fixed at the other end of the stirring plate through a screw, and the baffle seals the battery compartment.|[0015] A production device of a carbon-fixing wall surface heat-insulating material comprises the stirring assembly.|[0016] Compared with the prior art, the invention has the beneficial effects that:|[0017] The stirring assembly and the carbon-fixing wall surface heat-insulating material production equipment provided by the invention adopt the mounting assembly to be matched with the locking assembly, so that the stirring plate can be detachably mounted on a traditional stirring shaft, the deformed stirring plate can be independently replaced at the later stage conveniently, and the material conveying mechanism is additionally arranged on the stirring plate, so that the materials at the horizontal height of the stirring plate are conveyed to the upper side and the lower side, and the uniformity of the mixed materials of the stirring plate is improved. |DRAWINGS DESCRIPTION|[0018] FIG. 1 is a schematic diagram of the structure of the present invention;|[0019] FIG. 2 is an enlarged schematic view of the structure A in FIG. 1; |[0020] FIG. 3 is a schematic view of the structure of the baffle plate of the present invention after installation; |[0021] FIG. 4 is a schematic view of the structure of the present invention in semi-section; |[0022] FIG. 5 is a schematic view of a stirring plate structure according to the present invention; |[0023] FIG. 6 is a schematic view of a ferrule plate structure according to the present invention; |[0024] FIG. 7 shows the present invention a protective cover structure schematic diagram; |[0025] fig. 8 is a schematic view of a connector assembly according to the present invention. |[0026] In the figure, a stirring plate 1, a hoop plate 2, an embedding groove 3, a rubber clamping strip 4, a positioning inserting block 5, a reserved groove 6, a connecting inserting groove 7, a connecting inserting piece 8, a penetrating opening 9, a stop block 10, an elastic traction belt 11, a mounting opening 12, a slitting knife plate 13, a mounting groove 14, a motor 15, a sealing plate 16, a spiral material conveying shaft 17, a protective cover 18, a supporting column 19, a discharge opening 20, a material guiding pipe 21, a battery bin 22, a storage battery 23 and a baffle 24.|INVENTION MODE|Detailed Description|[0027] In order to make the objects, technical solutions, and advantages of the present invention more apparent, the embodiments of the present invention will be further described in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are some, but not all, embodiments of the present invention, are intended to be illustrative only and not limiting of the embodiments of the present invention, and that all other embodiments obtained by persons of ordinary skill in the art without making any inventive effort are within the scope of the present invention.|[0028] Example 1|[0029] Referring to fig. 1, 3-5, the invention provides a technical scheme that the stirring assembly comprises a stirring plate 1, wherein one end of the stirring plate 1 is provided with a mounting assembly, the surface of the mounting assembly is provided with a locking assembly, the surface of the stirring plate 1 is provided with a crushing assembly for crushing caking materials, the other end of the stirring plate 1 is provided with a material conveying mechanism for dispersing and mixing the materials at the other end of the stirring plate 1 on the upper side and the lower side, the mounting assembly is matched with the locking assembly to realize the detachable mounting of the stirring plate 1 on a traditional stirring shaft so as to facilitate the independent replacement of the deformed stirring plate 1 at the later stage, and the stirring plate 1 is additionally provided with a material conveying mechanism so as to realize the upward and downward conveying of the materials at the horizontal height of the stirring plate 1, thereby being beneficial to improving the uniformity of the mixed materials of the stirring plate 1.|[0030] Example two|[0031] Referring to fig. 2, 6 and 8, in order to mount the stirring plate 1 on the conventional stirring shaft in a hanging manner, the surface of the stirring shaft is provided with holes for inserting the positioning inserts 5 in advance, the mounting assembly comprises a hoop plate 2, an embedding groove 3, a rubber clamping strip 4 and the positioning inserts 5, the positioning inserts 5 are fixed on the inner ring surface of the hoop plate 2, the embedding groove 3 is provided with two groups, the two groups of the embedding grooves 3 are symmetrically distributed about the positioning inserts 5, the two groups of the embedding grooves 3 are all arranged on the inner ring surface of the hoop plate 2, the rubber clamping strip 4 is fixed in the embedding groove 3, the width of the rubber clamping strip 4 is larger than the depth of the embedding groove 3, the locking assembly comprises a reserved groove 6, a connecting slot 7, a connecting insert 8, a through hole 9, a stop block 10 and an elastic traction belt 11, the reserved groove 6 is provided with two groups, the two groups of reserved slots 6 are respectively arranged on the top surfaces of the plate bodies at the two ends of the hoop plate 2, the connecting slots 7 are arranged on the bottom surfaces of the reserved slots 6, the connecting plug-in unit 8 is in a pi-shaped plate structure, the connecting plug-in unit 8 comprises two parallel side plates and top plates fixed on the two groups of side plates, the two parallel side plates of the connecting plug-in unit 8 are respectively movably inserted into the two groups of connecting slots 7, the top plates of the connecting plug-in unit 8 are lapped on the reserved slots 6, the through holes 9 are arranged on the end plate bodies of the hoop plate 2, the through holes 9 are in one-to-one correspondence with the reserved slots 6, the through holes 9 are communicated with the reserved slots 6, the stop blocks 10 are movably inserted into the through holes 9, the stop blocks 10 penetrate into the reserved slots 6 after penetrating through the through holes 9, and when the top plates of the connecting plug-in unit 8 are lapped on the reserved slots 6, the stop blocks 10 are positioned above the top plates of the connecting plug-in unit 8, so that the anti-drop limit of the connecting plug-in unit 8 is realized; the top surface of one end of the stop block 10 extending into the reserved groove 6 is provided with an inclined surface, the other end center of the stop block 10 is fixed on a crossing node of the elastic traction belt 11, the elastic traction belt 11 is of a cross-shaped platy structure, and four ends of the elastic traction belt 11 are fixed on the surface of the end plate body of the hoop plate 2.|[0032] The hoop plate 2 is broken off from the both ends of hoop plate 2 and detained on traditional (mixing) shaft, in this process, with the hole that locating insert 5 aimed at (mixing) shaft surface and offer, constitute the screens structure, then push down connecting insert 8 along dog 10's inclined plane, dog 10 slides along wearing mouth 9 and stretch-draw elasticity traction belt 11, connecting insert 8's curb plate inserts behind the connection slot 7, connecting insert 8's roof overlap joint is after reserving groove 6, elasticity traction belt 11 resilience traction dog 10 resets, dog 10 keeps off in connecting insert 8's one side, avoid connecting insert 8's curb plate to slide out from connecting slot 7, so realize connecting insert 8 and connect hoop plate 2's both ends plate body, and hoop plate 2 fixes on the (mixing) shaft.|[0033] Example III|[0034] On the basis of the second embodiment, in order to crush the lump materials in the stirring plate process, the crushing assembly comprises a mounting opening 12 and a cutting knife plate 13, the mounting opening 12 is formed in the surface of the stirring plate 1, the mounting opening 12 is provided with a plurality of mounting openings 12, the plurality of mounting openings 12 are distributed along the long edge of the stirring plate 1, the cutting knife plate 13 is of a diamond cylinder structure, the cutting knife plate 13 is fixed on the surface of the mounting opening 12, the cutting edge of the cutting knife plate 13 protrudes out of the mounting opening 12, and in the process that the stirring plate 1 rotates along with a stirring shaft, the cutting edge of the cutting knife plate 13 cuts up the lump materials.|[0035] Example IV|[0036] Referring to fig. 7, on the basis of the third embodiment, in order to disperse the materials at the horizontal height of the stirring plate 1 on the upper and lower sides, the material conveying mechanism comprises a mounting groove 14, a motor 15, a sealing plate 16, a spiral material conveying shaft 17, a protection cover 18, a support column 19, a material outlet 20 and a material guiding pipe 21, wherein the mounting groove 14 is provided with two groups, the two groups of mounting grooves 14 are respectively arranged on the top surface of the stirring plate 1 and the bottom surface of the stirring plate 1, the motor 15 is fixed in the mounting groove 14, the shaft body of the motor 15 penetrates through the inner ring opening of the sealing plate 16, the sealing plate 16 is in an annular plate-shaped structure, the sealing plate 16 is fixed at the notch of the mounting groove 14, the spiral material conveying shaft 17 is fixed on the shaft body of the motor 15, the protection cover 18 is sleeved outside the spiral material conveying shaft 17, one end of the protection cover 18 is fixed with a plurality of support columns 19, one end of each support column 19 is fixed on the surface of the stirring plate 1, the material outlet 20 is arranged on the surface of the protection cover 18, the material guiding pipe 21 is fixed on the outer wall of the protection cover 18, the material guiding pipe 21 is communicated with the protection cover 18, and the other end of the stirring plate 1 is provided with a power supply component for supplying power to the motor 15; the power supply assembly comprises a battery bin 22, a storage battery 23 and a baffle 24, wherein the battery bin 22 is arranged at the other end of the stirring plate 1, the storage battery 23 is fixed in the battery bin 22, the storage battery 23 is connected with the motor 15 through a wire, the baffle 24 is fixed at the other end of the stirring plate 1 through a screw, and the baffle 24 seals the battery bin 22;|[0037] In the process that the stirring plate 1 rotates along with the stirring shaft to mix materials, the motor 15 is started to drive the spiral conveying shaft 17 to rotate, the spiral conveying shaft 17 conveys materials close to the stirring plate 1 to the discharge port 20, and the conveyed materials are discharged through the material guiding pipe 21, so that the materials at the horizontal height of the stirring plate 1 are dispersed to two sides in the vertical direction, and the uniformity of material mixing is convenient to improve. |[0038] Example five|[0039] A production device of a carbon-fixing wall surface heat-insulating material comprises a stirring assembly.|[0040] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. (CN116272480)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of stirring plates, in particular to a stirring assembly and carbon-fixing wall surface heat-insulating material production equipment.|BACKGROUND ART|[0002] Carbon sequestration refers to measures to increase the carbon content of a carbon reservoir other than the atmosphere. Including physical carbon fixation and biological carbon fixation. Physical carbon sequestration is the long term storage of carbon dioxide in mined oil and gas wells, coal seams, and deep seas. Biosolids are the conversion of carbon dioxide in the atmosphere, which is inorganic carbon, to organic carbon, which is carbohydrate, and are immobilized in plants or in soil.|[0003] In the prior art, the wall heat-insulating material (also called as inorganic active wall heat-insulating material) can save a large amount of wall materials, improve the heat-insulating performance of the wall, save resources and reduce environmental pollution, is a novel material for heat insulation of inner and outer walls, and can be used for most structures of any building by using the wooden material, thereby achieving the purpose of carbon fixation. The aim of reducing carbon emission is fulfilled. The maximum potential for carbon sequestration can be achieved in exterior walls, floors and roof structures. For example, passive rooms designed for cold climates have two alternate building exterior wall systems, wood frame walls filled with insulation and concrete walls insulated with EPS exterior insulation. When the carbon-fixing wall surface heat-insulating material is produced, the materials are mixed by virtue of a stirring shaft.|[0004] But the equal fixed welding of stirring board on traditional (mixing) shaft surface is on the (mixing) shaft, when the stirring board long-term use appears warping and influences the stirring effect, is inconvenient for changing single stirring board, and when traditional stirring board rotates along with the (mixing) shaft, only can realize stirring board place level's material and mix, is inconvenient for promoting stirring homogeneity.|DISCLOSURE|Disclosure of Invention|[0005] The invention aims to provide a stirring assembly and carbon-fixing wall surface heat-insulating material production equipment so as to solve the problems in the background technology.|[0006] In order to achieve the purpose, the stirring assembly comprises a stirring plate, wherein one end of the stirring plate is provided with a mounting assembly, the surface of the mounting assembly is provided with a locking assembly, the surface of the stirring plate is provided with a crushing assembly for crushing caking materials, the other end of the stirring plate is provided with a material conveying mechanism, and the materials at the other end of the stirring plate are dispersed and mixed on the upper side and the lower side.|[0007] Preferably, the installation component includes hoop board, embedded groove, rubber clip strip and location inserted block, and the location inserted block is fixed on the interior anchor ring of hoop board, and the embedded groove is equipped with two sets of, and two sets of embedded grooves are about the location inserted block symmetric distribution, and two sets of embedded grooves all offer on the interior anchor ring of hoop board, and the rubber clip strip is fixed in the embedded groove, and the width of rubber clip strip is greater than the degree of depth of embedded groove.|[0008] Preferably, the locking assembly comprises two reserved grooves, connecting slots, connecting plug-ins, penetrating openings, stop blocks and elastic traction belts, wherein the two reserved grooves are respectively arranged on the top surfaces of plate bodies at two ends of the hoop plate, the connecting slots are respectively arranged on the bottom surfaces of the reserved grooves, the connecting plug-ins are of a pi-shaped plate structure, the connecting plug-ins comprise two side plates which are distributed in parallel and top plates which are fixed on the two groups of side plates, the two side plates which are distributed in parallel of the connecting plug-ins are respectively movably inserted into the two groups of connecting slots, and the top plates of the connecting plug-ins are lapped on the reserved grooves.|[0009] Preferably, the wearing mouth is arranged on the end plate body of the hooping plate, the wearing mouth corresponds to the reserved groove one by one, the wearing mouth is communicated with the reserved groove, the stop block is movably inserted into the wearing mouth, the stop block penetrates through the wearing mouth and then stretches into the reserved groove, when the top plate of the connecting plug-in unit is lapped on the reserved groove, the stop block is positioned above the top plate of the connecting plug-in unit, and the anti-drop limit of the connecting plug-in unit is realized.|[0010] Preferably, the top surface of one end of the stop block extending into the reserved groove is provided with an inclined plane, the center of the other end of the stop block is fixed on a cross joint of the elastic traction belt, the elastic traction belt is of a cross-shaped platy structure, and four ends of the elastic traction belt are fixed on the surface of an end plate body of the hoop plate.|[0011] Preferably, the crushing assembly comprises a mounting opening and a slitting knife plate, wherein the mounting opening is formed in the surface of the stirring plate, a plurality of mounting openings are formed in the mounting opening, the mounting openings are distributed along the long side of the stirring plate, the slitting knife plate is of a diamond cylinder structure, the slitting knife plate is fixed on the surface of the mounting opening, and the cutting edge of the slitting knife plate protrudes out of the mounting opening.|[0012] Preferably, the conveying mechanism comprises a mounting groove, a motor, a sealing plate, a spiral conveying shaft, a protective cover, a support column, a discharge hole and a material guiding pipe, wherein the mounting groove is provided with two groups, the two groups of mounting grooves are respectively formed in the top surface of the stirring plate and the bottom surface of the stirring plate, the motor is fixed in the mounting groove, a shaft body of the motor penetrates through an inner ring opening of the sealing plate, the sealing plate is of an annular plate-shaped structure, the sealing plate is fixed at a notch of the mounting groove, and the spiral conveying shaft is fixed on the shaft body of the motor.|[0013] Preferably, the protective cover is sleeved on the outer side of the spiral conveying shaft, one end of the protective cover is fixed with a plurality of support columns, one end of each support column is fixed on the surface of the stirring plate, the discharge hole is formed in the surface of the protective cover, the material guiding pipe is fixed on the outer wall of the protective cover, the material guiding pipe is communicated with the protective cover, and the other end of the stirring plate is provided with a power supply assembly for supplying power to the motor.|[0014] Preferably, the power supply assembly comprises a battery compartment, a storage battery and a baffle, wherein the battery compartment is arranged at the other end of the stirring plate, the storage battery is fixed in the battery compartment, the storage battery is connected with the motor through a wire, the baffle is fixed at the other end of the stirring plate through a screw, and the baffle seals the battery compartment.|[0015] A production device of a carbon-fixing wall surface heat-insulating material comprises the stirring assembly.|[0016] Compared with the prior art, the invention has the beneficial effects that:|[0017] The stirring assembly and the carbon-fixing wall surface heat-insulating material production equipment provided by the invention adopt the mounting assembly to be matched with the locking assembly, so that the stirring plate can be detachably mounted on a traditional stirring shaft, the deformed stirring plate can be independently replaced at the later stage conveniently, and the material conveying mechanism is additionally arranged on the stirring plate, so that the materials at the horizontal height of the stirring plate are conveyed to the upper side and the lower side, and the uniformity of the mixed materials of the stirring plate is improved. |DRAWINGS DESCRIPTION|[0018] FIG. 1 is a schematic diagram of the structure of the present invention;|[0019] FIG. 2 is an enlarged schematic view of the structure A in FIG. 1; |[0020] FIG. 3 is a schematic view of the structure of the baffle plate of the present invention after installation; |[0021] FIG. 4 is a schematic view of the structure of the present invention in semi-section; |[0022] FIG. 5 is a schematic view of a stirring plate structure according to the present invention; |[0023] FIG. 6 is a schematic view of a ferrule plate structure according to the present invention; |[0024] FIG. 7 shows the present invention a protective cover structure schematic diagram; |[0025] fig. 8 is a schematic view of a connector assembly according to the present invention. |[0026] In the figure, a stirring plate 1, a hoop plate 2, an embedding groove 3, a rubber clamping strip 4, a positioning inserting block 5, a reserved groove 6, a connecting inserting groove 7, a connecting inserting piece 8, a penetrating opening 9, a stop block 10, an elastic traction belt 11, a mounting opening 12, a slitting knife plate 13, a mounting groove 14, a motor 15, a sealing plate 16, a spiral material conveying shaft 17, a protective cover 18, a supporting column 19, a discharge opening 20, a material guiding pipe 21, a battery bin 22, a storage battery 23 and a baffle 24.|INVENTION MODE|Detailed Description|[0027] In order to make the objects, technical solutions, and advantages of the present invention more apparent, the embodiments of the present invention will be further described in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are some, but not all, embodiments of the present invention, are intended to be illustrative only and not limiting of the embodiments of the present invention, and that all other embodiments obtained by persons of ordinary skill in the art without making any inventive effort are within the scope of the present invention.|[0028] Example 1|[0029] Referring to fig. 1, 3-5, the invention provides a technical scheme that the stirring assembly comprises a stirring plate 1, wherein one end of the stirring plate 1 is provided with a mounting assembly, the surface of the mounting assembly is provided with a locking assembly, the surface of the stirring plate 1 is provided with a crushing assembly for crushing caking materials, the other end of the stirring plate 1 is provided with a material conveying mechanism for dispersing and mixing the materials at the other end of the stirring plate 1 on the upper side and the lower side, the mounting assembly is matched with the locking assembly to realize the detachable mounting of the stirring plate 1 on a traditional stirring shaft so as to facilitate the independent replacement of the deformed stirring plate 1 at the later stage, and the stirring plate 1 is additionally provided with a material conveying mechanism so as to realize the upward and downward conveying of the materials at the horizontal height of the stirring plate 1, thereby being beneficial to improving the uniformity of the mixed materials of the stirring plate 1.|[0030] Example two|[0031] Referring to fig. 2, 6 and 8, in order to mount the stirring plate 1 on the conventional stirring shaft in a hanging manner, the surface of the stirring shaft is provided with holes for inserting the positioning inserts 5 in advance, the mounting assembly comprises a hoop plate 2, an embedding groove 3, a rubber clamping strip 4 and the positioning inserts 5, the positioning inserts 5 are fixed on the inner ring surface of the hoop plate 2, the embedding groove 3 is provided with two groups, the two groups of the embedding grooves 3 are symmetrically distributed about the positioning inserts 5, the two groups of the embedding grooves 3 are all arranged on the inner ring surface of the hoop plate 2, the rubber clamping strip 4 is fixed in the embedding groove 3, the width of the rubber clamping strip 4 is larger than the depth of the embedding groove 3, the locking assembly comprises a reserved groove 6, a connecting slot 7, a connecting insert 8, a through hole 9, a stop block 10 and an elastic traction belt 11, the reserved groove 6 is provided with two groups, the two groups of reserved slots 6 are respectively arranged on the top surfaces of the plate bodies at the two ends of the hoop plate 2, the connecting slots 7 are arranged on the bottom surfaces of the reserved slots 6, the connecting plug-in unit 8 is in a pi-shaped plate structure, the connecting plug-in unit 8 comprises two parallel side plates and top plates fixed on the two groups of side plates, the two parallel side plates of the connecting plug-in unit 8 are respectively movably inserted into the two groups of connecting slots 7, the top plates of the connecting plug-in unit 8 are lapped on the reserved slots 6, the through holes 9 are arranged on the end plate bodies of the hoop plate 2, the through holes 9 are in one-to-one correspondence with the reserved slots 6, the through holes 9 are communicated with the reserved slots 6, the stop blocks 10 are movably inserted into the through holes 9, the stop blocks 10 penetrate into the reserved slots 6 after penetrating through the through holes 9, and when the top plates of the connecting plug-in unit 8 are lapped on the reserved slots 6, the stop blocks 10 are positioned above the top plates of the connecting plug-in unit 8, so that the anti-drop limit of the connecting plug-in unit 8 is realized; the top surface of one end of the stop block 10 extending into the reserved groove 6 is provided with an inclined surface, the other end center of the stop block 10 is fixed on a crossing node of the elastic traction belt 11, the elastic traction belt 11 is of a cross-shaped platy structure, and four ends of the elastic traction belt 11 are fixed on the surface of the end plate body of the hoop plate 2.|[0032] The hoop plate 2 is broken off from the both ends of hoop plate 2 and detained on traditional (mixing) shaft, in this process, with the hole that locating insert 5 aimed at (mixing) shaft surface and offer, constitute the screens structure, then push down connecting insert 8 along dog 10's inclined plane, dog 10 slides along wearing mouth 9 and stretch-draw elasticity traction belt 11, connecting insert 8's curb plate inserts behind the connection slot 7, connecting insert 8's roof overlap joint is after reserving groove 6, elasticity traction belt 11 resilience traction dog 10 resets, dog 10 keeps off in connecting insert 8's one side, avoid connecting insert 8's curb plate to slide out from connecting slot 7, so realize connecting insert 8 and connect hoop plate 2's both ends plate body, and hoop plate 2 fixes on the (mixing) shaft.|[0033] Example III|[0034] On the basis of the second embodiment, in order to crush the lump materials in the stirring plate process, the crushing assembly comprises a mounting opening 12 and a cutting knife plate 13, the mounting opening 12 is formed in the surface of the stirring plate 1, the mounting opening 12 is provided with a plurality of mounting openings 12, the plurality of mounting openings 12 are distributed along the long edge of the stirring plate 1, the cutting knife plate 13 is of a diamond cylinder structure, the cutting knife plate 13 is fixed on the surface of the mounting opening 12, the cutting edge of the cutting knife plate 13 protrudes out of the mounting opening 12, and in the process that the stirring plate 1 rotates along with a stirring shaft, the cutting edge of the cutting knife plate 13 cuts up the lump materials.|[0035] Example IV|[0036] Referring to fig. 7, on the basis of the third embodiment, in order to disperse the materials at the horizontal height of the stirring plate 1 on the upper and lower sides, the material conveying mechanism comprises a mounting groove 14, a motor 15, a sealing plate 16, a spiral material conveying shaft 17, a protection cover 18, a support column 19, a material outlet 20 and a material guiding pipe 21, wherein the mounting groove 14 is provided with two groups, the two groups of mounting grooves 14 are respectively arranged on the top surface of the stirring plate 1 and the bottom surface of the stirring plate 1, the motor 15 is fixed in the mounting groove 14, the shaft body of the motor 15 penetrates through the inner ring opening of the sealing plate 16, the sealing plate 16 is in an annular plate-shaped structure, the sealing plate 16 is fixed at the notch of the mounting groove 14, the spiral material conveying shaft 17 is fixed on the shaft body of the motor 15, the protection cover 18 is sleeved outside the spiral material conveying shaft 17, one end of the protection cover 18 is fixed with a plurality of support columns 19, one end of each support column 19 is fixed on the surface of the stirring plate 1, the material outlet 20 is arranged on the surface of the protection cover 18, the material guiding pipe 21 is fixed on the outer wall of the protection cover 18, the material guiding pipe 21 is communicated with the protection cover 18, and the other end of the stirring plate 1 is provided with a power supply component for supplying power to the motor 15; the power supply assembly comprises a battery bin 22, a storage battery 23 and a baffle 24, wherein the battery bin 22 is arranged at the other end of the stirring plate 1, the storage battery 23 is fixed in the battery bin 22, the storage battery 23 is connected with the motor 15 through a wire, the baffle 24 is fixed at the other end of the stirring plate 1 through a screw, and the baffle 24 seals the battery bin 22;|[0037] In the process that the stirring plate 1 rotates along with the stirring shaft to mix materials, the motor 15 is started to drive the spiral conveying shaft 17 to rotate, the spiral conveying shaft 17 conveys materials close to the stirring plate 1 to the discharge port 20, and the conveyed materials are discharged through the material guiding pipe 21, so that the materials at the horizontal height of the stirring plate 1 are dispersed to two sides in the vertical direction, and the uniformity of material mixing is convenient to improve. |[0038] Example five|[0039] A production device of a carbon-fixing wall surface heat-insulating material comprises a stirring assembly.|[0040] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. Family Number|(105416955)|105416955|Abstract|(CN116272480B B)|The invention relates to the technical field of stirring plates , in particular to a stirring assembly and carbon -sequestration wall thermal insulation material production equipment , which comprises a stirring plate , one end of the stirring plate is provided with a mounting assembly , the surface of the mounting assembly is provided with a locking assembly , the surface of the stirring plate is provided with a crushing assembly , and the crushing assembly is used for crushing caked materials . A material conveying mechanism is arranged at the other end of the stirring plate and disperses and mixes materials at the other end of the stirring plate to the upper side and the lower side ; the stirring assembly and the carbon -sequestration wall thermal insulation material production equipment have the beneficial effects that the mounting assembly is adopted to be matched with the locking assembly , so that the stirring plate is detachably mounted on a traditional stirring shaft , and the deformed stirring plate can be independently replaced in the later period ; and the material conveying mechanism is additionally arranged on the stirring plate , so that the materials at the horizontal height of the stirring plate are conveyed to the upper side and the lower side , and the material mixing uniformity of the stirring plate is improved . |CPC codes|(CN116272480B B)|B01F - 027/112 |B01F - 027/171 |B01F - 035/717 |IPC codes|(CN116272480B B)|B01F - 027/112 |B01F - 027/171 |B01F - 035/71 |Title|(CN116272480 A)|Stirring assembly and carbon -sequestration wall thermal insulation material production equipment | Chemical engineering B01F-007/00/033|B01F-007/00/233|B01F-007/00/6|B01F-015/00/831|B01F-027/112|B01F-027/171|B01F-035/717|B01F-2215/0014|B01F-2215/0036|B01F-2215/0037|B01F-2215/0047|B01F-2215/005|Y02P-070/32 B01F-007/00/033|B01F-007/00/233|B01F-007/00/6|B01F-015/00/831|B01F-027/112|B01F-027/171|B01F-035/717|B01F-2215/0014|B01F-2215/0036|B01F-2215/0037|B01F-2215/0047|B01F-2215/005|Y02P-070/32 B01F-027/112|B01F-027/171|B01F-035/71 B01F-027/112|B01F-027/171|B01F-035/71 CN115920700|AU2020103888|CN111013428|CN210229714U|CN115962997|CN218047353U CN115920700 104487585 WHO=Examiner SELF=N CAT=A|AU2020103888 92707659 WHO=Examiner SELF=N CAT=A|CN111013428 88338933 WHO=Examiner SELF=N CAT=A|CN210229714U 88139306 WHO=Examiner SELF=N CAT=A|CN115962997 104581184 WHO=Examiner SELF=N|CN218047353U 103045881 WHO=Examiner SELF=N CN210229714U; CN111013428; AU2020103888; CN115920700; CN218047353U; CN115962997 GRANTED (CN116272480)|GRANTED ALIVE (CN116272480)|ALIVE (CN116272480)|LEGAL DETAILS FOR CN116272480|Actual or expected expiration date=2043-04-19|Legal state=ALIVE|Status=GRANTED|Event publication date=2023-04-19|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202310416466|Application date=2023-04-19|Standardized application number=2023CN-0416466|Event publication date=2023-06-23|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN116272480|Publication stage code=A|Publication date=2023-06-23|Standardized publication number=CN116272480|Event publication date=2023-06-23|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-07-11|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-07-11|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN116272480|Publication stage code=B|Publication date=2025-07-11|Standardized publication number=CN116272480B|Event publication date=2025-07-11|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN116272480)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRxf2/zsYL5Qxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000078141141&ekey=2163&xpn=CN116272480B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=yVnAWg7uVuIVJ4xolQ3TSrmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN116272480)|CN|(CN116272480)|CN (CN116272480)|NAME=THE SECOND CONSTRUCTION CO. LTD. OF CHINA CONSTRUCTION EIGHTH ENGINEERING DIVISION , COUNTRY=CN|(CN116272480)|NAME=THE SECOND CONSTRUCTION CO. LTD. OF CHINA CONSTRUCTION EIGHTH ENGINEERING DIVISION , COUNTRY=CN (CN116272480)|NAME=JIANG MING;JINAN XINDA PATENT OFFICE CO. LTD. , REG=37100|(CN116272480)|NAME=JIANG MING;JINAN XINDA PATENT OFFICE CO. LTD. , REG=37100 (CN116272480)|CN|(CN116272480)|CN (CN116272480)|NAME=ZHU RENJIE, COUNTRY=CN |NAME=LI CHAO|NAME=XU BEI|NAME=WANG DAWEI|NAME=JIA YUDONG|(CN116272480)|NAME=ZHU RENJIE, COUNTRY=CN |NAME=LI CHAO|NAME=XU BEI|NAME=WANG DAWEI|NAME=JIA YUDONG 0 1 Titre: (CN116272480)|Stirring assembly and carbon fixation wall insulation material production equipment Résumé: (CN116272480)|The invention relates to the technical field of stirring plates, in particular to a stirring assembly and carbon-sequestration wall thermal insulation material production equipment, which comprises a stirring plate, one end of the stirring plate is provided with a mounting assembly, the surface of the mounting assembly is provided with a locking assembly, the surface of the stirring plate is provided with a crushing assembly, and the crushing assembly is used for crushing caked materials. A material conveying mechanism is arranged at the other end of the stirring plate and disperses and mixes materials at the other end of the stirring plate to the upper side and the lower side; the stirring assembly and the carbon-sequestration wall thermal insulation material production equipment have the beneficial effects that the mounting assembly is adopted to be matched with the locking assembly, so that the stirring plate is detachably mounted on a traditional stirring shaft, and the deformed stirring plate can be independently replaced in the later period; and the material conveying mechanism is additionally arranged on the stirring plate, so that the materials at the horizontal height of the stirring plate are conveyed to the upper side and the lower side, and the material mixing uniformity of the stirring plate is improved. 11 Abstract gpt-4o-mini no The patent focuses on equipment for producing thermal insulation materials and does not address the accelerated weathering of minerals or CO₂ capture.
11 CN202410375034 CN202410375034 CN118270818 110457368 CN118270818 A 2024-07-02 [CN118270818] 2024-03-29 2024-03-29 2024-07-02 (CN118270818)|2044-03-29 (CN118270818)|High-capacity carbon sequestration biological material derived from oyster shells and preparation method of high-capacity carbon sequestration biological material (CN118270818)|The invention relates to a high-capacity carbon sequestration biological material derived from oyster shells and a preparation method of the high-capacity carbon sequestration biological material, and belongs to the field of biological materials. The preparation method comprises the following steps: by taking a byproduct oyster shell of mariculture oysters as a raw material, crushing the oyster shell to obtain oyster shell powder, mixing the oyster shell powder with a caustic soda aqueous solution, performing mechanochemical treatment in a ball mill, cleaning and drying a wet material, and performing microwave thermal decomposition in a microwave rapid ashing furnace to prepare the high-capacity carbon sequestration biological material with high activity and high specific surface area. The high-capacity carbon sequestration biological material is rich in raw material source, low in cost, simple in preparation process flow, energy-saving and environment-friendly, not only realizes resource utilization of the oyster shell waste residues, but also is high in carbon sequestration capacity, has remarkable economic and ecological benefits, and is suitable for industrial production. The method has important practical significance on sustainable development and green low-carbon economy of the oyster breeding industry. NANCHANG HANGKONG UNIVERSITY (CN118270818)|NANCHANG HANGKONG UNIVERSITY ([CN]) LU JINSHAN|WU JINAN|SHU JIAXIN|WANG FANGQIANG (CN118270818)|LU JINSHAN|WU JINAN|SHU JIAXIN|WANG FANGQIANG (CN118270818)|LIU AIFANG;NANCHANG QINGYUAN PATENT AGENT OFFICE (GENERAL PARTNERSHIP)|Reg. Nb: 36123 (CN118270818)|The method for preparing the carbon-fixing biological material by using a large amount of oyster shells generated by oyster cultivation has the advantages of rich and sustainable raw material sources, and the special honeycomb structure of the oyster shells enables the carbon-fixing biological material to have the carbon-fixing characteristics of high specific surface area, high activity and large capacity, so that the method provides technical guarantee for the value-added utilization of the oyster shells and the mass production of the carbon-fixing biological material.|The preparation method has the advantages of abundant raw material sources, low cost, simple preparation process flow, energy conservation and environmental protection, prepares the high-capacity carbon-fixing biological material, realizes the recycling of solid waste resources, can be used for absorbing carbon dioxide in the atmosphere, achieves the purpose of carbon fixing, has good economic and ecological benefits, and has important significance for realizing the double-carbon target and the sustainable development of the whole society.|The carbon fixing process is based on sea water condition, most occasions cannot utilize the carbon fixing agent, the carbon fixing agent is prepared by uniformly mixing calcined dolomite, magnesium chloride, calcium oxide and calcium chloride, the raw material preparation process is relatively complex, and the carbon fixing process is discontinuous.| (CN118270818)|1. The preparation method of the high-capacity carbon-fixing biological material from oyster shells comprises the following steps: step S1: crushing oyster shells to obtain oyster shell powder; Step S2: adding an aqueous solution of caustic soda into oyster shell powder, and performing mechanochemical treatment in a ball mill to obtain wet materials; step S3: washing and drying the wet material to obtain dried and fluffy oyster shell powder; Step S4: placing the fluffy oyster shell powder in a microwave rapid ashing furnace, and carrying out thermal decomposition at a certain temperature in an oxygen atmosphere to prepare the carbon-fixing biological material. | (CN118270818)|The invention aims to provide a high-capacity carbon-fixing biological material derived from oyster shells and a preparation method thereof.|The invention relates to a high-capacity carbon-fixing biological material derived from oyster shells and a preparation method thereof, belonging to the field of biological materials.|The patent CN201811351040.5 discloses a semi-closed energy conversion remote transmission and carbon fixation system taking magnesium as a carrier, wherein the carbon fixation process depends on redundant energy sources of renewable energy sources and magnesium produced by an electrolytic magnesium plant, the energy sources are unstable, meanwhile, raw material magnesium can reach a use place only by long-distance transportation, the energy consumption is higher, the carbon fixation system is limited to a larger extent, and the carbon fixation process cannot be continuous.| (CN118270818)|CARBON FIXING(100,27)|BIOLOGICAL MATERIAL(100,25)|OYSTER(100,23)|OYSTER SHELL(100,22)|CARBON FIXING BIOLOGICAL MATERIAL(100,17)|MARICULTURE OYSTER BYPRODUCT(63,2)|MICROWAVE RAPID ASHING FURNACE(58,9)|FLUFFY OYSTER(57,13)|OYSTER RESOURCE UTILIZATION(53,1)|ELECTROLYTIC MAGNESIUM PLANT(51,1)|ECOLOGICAL BENEFIT(48,2)|CALCINED DOLOMITE(48,1)|CRUSHING OYSTER(47,2)|RAPID ASHING FURNACE(44,9)|ECONOMIC BENEFIT(40,4)|SOCIETY SUSTAINABLE DEVELOPMENT(40,1)|MECHANO CHEMICAL TREATMENT(37,3)|DRIED OYSTER(35,3)|SIGNIFICANCE(33,2)|CAUSTIC SODA AQUEOUS SOLUTION(33,1)|OYSTER CULTIVATION INDUSTRY(33,1)|TECHNICAL GUARANTEE(32,1)|REALIZING SUSTAINABLE DEVELOPMENT(30,1)|CAUSTIC SODA(26,24)|SEAWATER CONDITION(26,1)|OYSTER SHELL HONEYCOMB STRUCTURE(25,1)|WASTE RESIDUE(24,1)|OCCASION(23,1)|AQUEOUS SOLUTION(22,1)|REALIZING DOUBLE CARBON TARGET(22,1)|OXYGEN ATMOSPHERE(21,4)|ABSORBING CARBON DIOXIDE(21,1)|CARBON FIXATION(20,12)|SUSTAINABLE DEVELOPMENT(20,1)|GAWGB APERTURE ADSORPTION TESTER(19,4)|THERMAL DECOMPOSITION(18,27)|CAUSTIC SODA SOLUTION(18,18)|THERMOGRAVIMETRIC ANALYZER(18,8)|OYSTER CULTIVATION(18,3)|RECYCLING(18,2)|TAIL GAS ABSORBENT(18,2)|ENERGY CONSERVATION(17,3)|ENVIRONMENTAL PROTECTION(17,3)|CLEANED OYSTER SHELL(15,4)|TRANSMITTING ENERGY CONVERSION(15,1)|BALL MILL(14,8)|SOLID WASTE RESOURCE(14,3)|TAIL GAS TREATMENT(14,2)|RICH(14,1)|CALCIUM CHLORIDE(13,1)|CARBON FIXING CAPACITY(13,1)|MAGNESIUM CHLORIDE(13,1)|CARBON FIXING(12,2)|REDUNDANT ENERGY SOURCE(12,1)|CAO TRAP(11,4)|CALCIUM OXIDE(11,1)|ABUNDANT RAW MATERIAL SOURCE(10,2)|OYSTER PARTICLE SIZE(10,2)|ENERGY CONVERSION(10,1)|LARGE CAPACITY(10,1)|ADSORPTION CAPACITY(9,4)|CAPTURE EXPERIMENT(9,4)|LARGE EXTENT(9,1)|LONG DISTANCE TRANSPORTATION(9,1)|MASS PRODUCTION(9,1)|RAW MATERIAL MAGNESIUM(9,1)|WET MATERIAL(8,11)|PREPARATION PROCESS FLOW(8,2)|CRUSHED OYSTER SHELL(8,1)|FLUFFY OYSTER SHELL(8,1)|GREEN LOW CARBON ECONOMY(8,1)|OCEAN RESOURCE UTILIZATION(8,1)|SUSTAINABLE RAW MATERIAL SOURCE(8,1)|VALUE ADDED UTILIZATION(8,1)|MICROWAVE THERMAL DECOMPOSITION(7,4)|ENERGY CONSUMPTION(7,3)|RAW MATERIAL SOURCE(7,3)|CARBON FIXATION(7,2)|HONEYCOMB STRUCTURE(7,2)|SEAWATER OYSTER CULTIVATION(7,1)|CAO CARBON FIXING(6,5)|SOLID WASTE(6,3)|OYSTER POWDER(6,2)|TRAPPED CAO VALUE(6,2)|BYPRODUCT OYSTER(6,1)|CHOICE TECHNOLOGY(6,1)|DECOMPOSE OYSTER(6,1)|ENERGY SOURCE(6,1)|MICROMOLECULAR PROTEIN(6,1)|RENEWABLE ENERGY SOURCE(6,1)|ADSORBENT(5,4)|BET(5,4)|CARBON FIXATION CAPACITY(5,4)|IMPURITY GAS(5,4)|SAMPLE VESSEL(5,4)|AIR POLLUTION PREVENTION(5,2)|ORGANISM PROTEIN(5,2)|CHINESE DOUBLE SHELL AQUACULTURE(5,1)|HUGE ASSISTANCE(5,1)|OYSTER PROPORTION(5,1)|PERMANENT SEQUESTRATION(5,1)|PYROLYSIS GASIFICATION TEMPERATURE(5,1)|WASTE ALKALI LIQUOR(5,1)|ORGANIC MATTER DECOMPOSITION(4,3)|ADHESIVENESS(4,2)|ALKALINE SOLUTION(4,2)|CALCIUM CARBONATE PARTICLE(4,2)|CALCIUM CARBONATE THERMAL DECOMPOSITION(4,2)|OYSTER THERMAL DECOMPOSITION TEMPERATURE(4,2)|CACO REACTION(4,1)|ENVIRONMENT POLLUTION(4,1)|MIXING OYSTER(4,1)|NEGATIVE ECOLOGICAL ENVIRONMENT INFLUENCE(4,1)|ADSORPTION REGENERATION PEAK VALUE(3,4)|STANDARD SAMPLE(3,4)|BALL MILLING TIME(3,3)|ANNUAL YIELD(3,1)|BIOLOGICAL MATERIAL FIELD(3,1)|BIOMASS(3,1)|CARBON FIXING BIOMATERIAL(3,1)|FOSSIL ENERGY(3,1)| (CN118270818)|1. The preparation method of the high-capacity carbon-fixing biological material from oyster shells comprises the following steps:| step S1: crushing oyster shells to obtain oyster shell powder; | Step S2: adding an aqueous solution of caustic soda into oyster shell powder, and performing mechanochemical treatment in a ball mill to obtain wet materials; | step S3: washing and drying the wet material to obtain dried and fluffy oyster shell powder; | Step S4: placing the fluffy oyster shell powder in a microwave rapid ashing furnace, and carrying out thermal decomposition at a certain temperature in an oxygen atmosphere to prepare the carbon-fixing biological material. |2. The method of manufacturing according to claim 1, characterized in that: in the step S1, the particle size of the oyster shell powder is 40-80 meshes.|3. The method of manufacturing according to claim 1, characterized in that: in the step S2, the concentration of the caustic soda solution is 0.1-1 mol/L, and the ball milling time is 0.5-2 h.|4. The method of manufacturing according to claim 1, characterized in that: in the step S4, the thermal decomposition temperature is 600-800 ℃, and the thermal decomposition time is 0.1-1 h.|5. The method of manufacturing according to claim 1, characterized in that: the caustic soda solution used in step S2 may be used to absorb the tail gas in step S4, and perform the tail gas treatment to prevent air pollution.|6. A high-capacity carbon-fixing biological material derived from oyster shells, which is characterized in that: a method of manufacture according to any one of claims 1 to 5. (CN118270818)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of biological materials, and particularly relates to a high-capacity carbon-fixing biological material derived from oyster shells and a preparation method thereof.|BACKGROUND ART|[0003] At present, the main way of absorbing carbon dioxide by nature is ocean and forest, the ocean area of the earth occupies 71 percent of the earth surface area, which is 2.4 times of the land area, and the reasonable utilization of ocean resources becomes a huge assistance for realizing double carbon. China is a large country for oyster cultivation, the resources are very rich, the production market is huge, the proportion of oyster shells accounts for 70% -95% of the wet weight of the oysters, and calcium carbonate reaches 90% -99% in the oyster shells. The average amount of calcium carbonate produced by Chinese double-shell aquaculture per year is approximately 800 ten thousand metric tons. Through double-shell aquaculture, a large amount of CO 2 in the seawater is absorbed, the seawater is stored in a CaCO 3 mode, the concentration of carbon dioxide in the seawater is reduced, the absorption of CO 2 in the air by the ocean is further enhanced, and the purpose of carbon fixation is achieved. However, after oysters are eaten, oyster shells are used as byproducts of mariculture oysters, the annual yield is huge, and efficient recycling is urgently needed. Therefore, the oyster shell is comprehensively recycled to produce high added value products, so that good economic benefits can be generated, solid waste resources can be reused, and negative ecological environment influence can be eliminated.|[0004] The CCUS (CO 2 capture, sequestration and utilization technology) can separate CO 2 from industrial processes, energy utilization or the atmosphere for direct utilization, or injection into a formation to achieve permanent sequestration of CO 2, is an important technological option for achieving low-carbon utilization of fossil energy. The invention patent CN202410129929.8 discloses a seawater-based repeated efficient carbon fixing method, which comprises the steps of introducing carbon dioxide-containing gas into seawater, adding a carbon fixing agent for activation when the pH value of the carbon dioxide-containing gas is lower than 6.8, obtaining an alkaline solution containing Ca 2+、Mg2+ ions, and introducing the carbon dioxide-containing gas into the alkaline solution for carbon fixing. The carbon fixing process is based on sea water condition, most occasions cannot utilize the carbon fixing agent, the carbon fixing agent is prepared by uniformly mixing calcined dolomite, magnesium chloride, calcium oxide and calcium chloride, the raw material preparation process is relatively complex, and the carbon fixing process is discontinuous. The patent CN201811351040.5 discloses a semi-closed energy conversion remote transmission and carbon fixation system taking magnesium as a carrier, wherein the carbon fixation process depends on redundant energy sources of renewable energy sources and magnesium produced by an electrolytic magnesium plant, the energy sources are unstable, meanwhile, raw material magnesium can reach a use place only by long-distance transportation, the energy consumption is higher, the carbon fixation system is limited to a larger extent, and the carbon fixation process cannot be continuous. The invention patent CN202311330588.2 discloses a microalgae carbon fixing device and a carbon fixing method, wherein the microalgae periodically supplements a strengthening culture medium into circulating water and introduces mixed gas containing CO 2 in the culture process, so that the microalgae grow at a high speed and have high biomass concentration in an optimal feeding mode, and the microalgae can be used for fixing higher CO 2 in a short time so as to achieve the aim of biological carbon fixing. The method for carbon fixation has higher requirements on microalgae, can be optimized only by meeting various indexes, achieves the aim of carbon fixation, is greatly influenced by factors such as environment, has higher cost, and has a non-concise and continuous carbon fixation process.|[0005] The method for preparing the carbon-fixing biological material by using a large amount of oyster shells generated by oyster cultivation has the advantages of rich and sustainable raw material sources, and the special honeycomb structure of the oyster shells enables the carbon-fixing biological material to have the carbon-fixing characteristics of high specific surface area, high activity and large capacity, so that the method provides technical guarantee for the value-added utilization of the oyster shells and the mass production of the carbon-fixing biological material.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to provide a high-capacity carbon-fixing biological material derived from oyster shells and a preparation method thereof. The method is characterized in that a byproduct oyster shell of sea water oyster cultivation is used as a raw material, and the high-capacity carbon-fixing biological material with high activity and high specific surface area is prepared through the process steps of mixing oyster shell powder obtained by crushing oyster shells with caustic soda solution, ball milling by a mechanochemical method, cleaning and drying wet materials, microwave thermal decomposition and the like. The preparation method has the advantages of abundant raw material sources, low cost, simple preparation process flow, energy conservation and environmental protection, prepares the high-capacity carbon-fixing biological material, realizes the recycling of solid waste resources, can be used for absorbing carbon dioxide in the atmosphere, achieves the purpose of carbon fixing, has good economic and ecological benefits, and has important significance for realizing the double-carbon target and the sustainable development of the whole society.|[0007] The oyster powder is added into caustic soda solution for mechanochemical treatment, so that the oyster powder can catalyze and hydrolyze organic proteins in oyster shells and decompose the organic proteins into small molecular weight proteins or polypeptides linked by a plurality of amino acids. After the protein in the oyster shell is hydrolyzed, the adhesiveness among calcium carbonate particles in the oyster shell is greatly reduced, and the oyster shell powder obtained by washing and drying is fluffier, so that the oyster shell powder has the characteristics of higher specific surface area, high activity and the like while retaining a honeycomb structure. By adopting microwave heat treatment, the heating efficiency is greatly improved, the simultaneous heating of the inside and the outside of the oyster shell powder can be ensured, collapse caused by uneven heating of the structure is avoided, the specific surface area and the activity are reduced, and the carbon fixing capability of the product is ensured to the greatest extent. In the microwave thermal decomposition stage, chemical reactions such as thermal decomposition of calcium carbonate and hydrolyzed protein, treatment of waste gas generated by thermal decomposition and the like are performed, so that the tail gas is prevented from being discharged into the atmosphere to pollute the environment.|[0008] (1) Calcium carbonate decomposition reaction|[0009] |[0010] (2) Protein decomposition reaction|[0011] |[0012] (3) C, N, S oxide tail gas treatment|[0013] CO2+2NaOH→Na2CO3+H2O|[0014] 2NO2+2NaOH→NaNO3+NaNO2+H2O|[0015] SO2+2NaOH→Na2SO3+H2O|[0016] The invention provides a preparation method of a high-capacity carbon-fixing biological material derived from oyster shells, which comprises the following steps:|[0017] Step S1: preparing oyster shell into oyster shell powder; |[0018] Step S2: adding caustic soda solution into oyster shell powder, ball milling in a ball mill, and uniformly mixing to obtain wet materials; |[0019] step S3: washing and drying the wet material to obtain dried and fluffy oyster shells; |[0020] Step S4: placing the fluffy oyster shell powder in a microwave rapid ashing furnace, and carrying out thermal decomposition at a certain temperature in an oxygen atmosphere to release carbon, nitrogen and sulfur oxide gases to obtain a carbon-fixing biological material; |[0021] further, in the step S1, the particle size of the oyster shell powder is 40-80 mesh screen; |[0022] further, in the step S2, the concentration of the caustic soda solution is 0.1-1 mol/L, and the ball milling time is 0.5-2 h; |[0023] further, in the step S4, the thermal decomposition temperature of the oyster shell powder is 600-800 ℃ and the thermal decomposition time is 0.1-1 h; |[0024] Further, the caustic soda solution used in step S2 may be used to absorb the tail gas in step S4, and perform the tail gas treatment to prevent air pollution. |[0025] The invention has the beneficial effects that:|[0026] (1) The invention uses oyster shell waste with high yield and not effectively utilized as raw materials, has rich sources of raw materials, not only recycles solid waste resources, but also generates certain economic benefit, and improves the civil and environmental problems. |[0027] (2) The invention uses caustic soda solution to hydrolyze protein in oyster shell into micromolecular protein or polypeptide, reduces the adhesiveness between calcium carbonate particles, is convenient for complete thermal decomposition of calcium carbonate and organic matters in the micro-blog thermal decomposition stage, and the obtained CaO carbon-fixing biological material has higher specific surface area and activity.|[0028] (3) The ball milling and microwave thermal decomposition of the invention belongs to short-time low-energy-consumption process steps, oxygen is introduced during thermal decomposition, so as to ensure the complete decomposition of calcium carbonate, protein and the like, and the oyster powder alkali treatment solution is utilized to absorb waste gas generated by the microwave thermal decomposition, thereby preventing tail gas from polluting air.|[0029] (4) The invention adopts a microwave rapid ashing furnace to thermally decompose oyster shell powder treated by caustic soda solution, and microwave heating belongs to an internal heat source method, so that the temperature rising speed is high, the oyster shell powder is uniformly heated as a whole, the high specific surface area of the oyster shell powder is reserved, the high activity of the oyster shell powder is maintained, and the thermal decomposition efficiency is high.|DRAWINGS DESCRIPTION|[0030] FIG. 1 is a process flow of preparing a high-capacity carbon-fixing biomaterial derived from oyster shells.|INVENTION MODE|Detailed Description|[0031] In order that the above-recited objects, features and advantages of the invention will be more clearly understood, a more particular description of the invention will be rendered by reference to specific embodiments thereof. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways than those described herein, and therefore the present invention is not limited to the specific embodiments disclosed below.|[0032] Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this application pertains. The terms "first," "second," and the like in the description and in the claims, are not used for any order, quantity, or importance, but are used for distinguishing between different elements. Likewise, the terms "a" or "an" and the like do not denote a limitation of quantity, but rather denote the presence of at least one.|[0033] As shown in fig. 1, a preparation method of a high-capacity carbon-fixing biological material derived from oyster shells comprises the following steps:|[0034] step S1: preparing oyster shell into oyster shell powder, and sieving with a 40-80 mesh sieve; |[0035] step S2: adding caustic soda solution into oyster shell powder, ball milling in a ball mill, and uniformly mixing to obtain wet materials, wherein the concentration of the caustic soda is 0.1 mol/L-1 mol/L, and the ball milling time is 0.5-2 h; |[0036] step S3: washing and drying the wet material to obtain dried and fluffy oyster shell powder; |[0037] step S4: placing the fluffy oyster shell powder in a microwave rapid ashing furnace, carrying out thermal decomposition at a certain temperature in an oxygen atmosphere to release carbon, nitrogen and sulfur oxide gases, wherein the remainder is a carbon-fixing biological material, the thermal decomposition temperature of the oyster shell powder is 600-800 ℃, the thermal decomposition time is 0.1-1 h, and the released tail gas is absorbed by waste alkali liquor in the step S2; |[0038] Example 1 |[0039] Crushing the cleaned oyster shells, ball-milling the crushed oyster shells in a ball mill for 1h through a 40-mesh screen, cleaning and drying the obtained material to obtain fluffy oyster shell powder, then placing the fluffy oyster shell powder in a microwave rapid ashing furnace which is introduced with oxygen atmosphere, carrying out thermal decomposition for 0.1h at 600 ℃, absorbing and releasing impurity gases such as CO 2、NO2、SO2 by using waste caustic soda solution, and obtaining the remainder which is the high-capacity CaO carbon-fixing biological material.|[0040] The specific surface area is measured by a BK122T-B GAWGB aperture adsorption tester and calculated by a BET method, and the carbon fixation capacity is measured by performing a CO 2 absorption and capture experiment on a thermogravimetric analyzer. The specific surface area is measured by a comparison method, a standard sample with known specific surface area is adopted to compare the sample of the adsorbent to be measured in the parallel gas path, the specific surface area value of the adsorbent to be measured can be read out according to the multiple relation of adsorption/regeneration peak values on a computer, and the CaO specific surface area is measured to be 3.13m 2/g. Weighing a certain amount of CaO, placing the CaO in a sample vessel, heating the CaO to 600-650 ℃ in a thermogravimetric analyzer, keeping the temperature for 10min, and introducing CO 2 gas, wherein the weight gain corresponds to the amount of trapped CO 2 because the CaO traps CO 2 and is converted into CaCO 3, and the capacity of the trapped CO 2 is calculated to be 0.209g/g, so that the theoretical adsorption capacity is 26% (the theoretical value of the trapped CO 2 of CaO is 0.789 g/g).|[0041] Example 2|[0042] Crushing the cleaned oyster shells, sieving with a 40-mesh sieve, adding caustic soda solution with caustic soda concentration of 0.5mol/L, ball milling for 2 hours in a ball mill, decomposing organic matters on the surfaces of the oyster shells, and hydrolyzing proteins to obtain wet materials. Cleaning and drying wet materials to obtain fluffy oyster shell powder, then placing the fluffy oyster shell powder in a microwave rapid ashing furnace which is filled with oxygen, carrying out thermal decomposition for 0.3h at 650 ℃, absorbing and releasing impurity gases such as CO 2、NO2、SO2 by using waste caustic soda solution, and obtaining the remainder which is the high-capacity CaO carbon-fixing biological material.|[0043] The specific surface area is measured by a BK122T-B GAWGB aperture adsorption tester and calculated by a BET method, and the carbon fixation capacity is measured by performing a CO 2 absorption and capture experiment on a thermogravimetric analyzer. The specific surface area is measured by a comparison method, a standard sample with known specific surface area is adopted to compare the sample of the adsorbent to be measured in a parallel gas path, the specific surface area value of the adsorbent to be measured can be read out according to the multiple relation of adsorption/regeneration peak values on a computer, and the CaO specific surface area is measured to be 9.24m 2/g. Weighing a certain amount of CaO, placing the CaO in a sample vessel, heating the CaO to 600-650 ℃ in a thermogravimetric analyzer, keeping the temperature for 10min, and introducing CO 2 gas, wherein the weight gain corresponds to the amount of trapped CO 2 because the CaO traps CO 2 and is converted into CaCO 3, and calculating the capacity of trapped CO 2 to reach 48% of theoretical adsorption capacity (the theoretical value of the trapped CaO CO 2 is 0.789 g/g).|[0044] Example 3|[0045] Crushing the cleaned oyster shells, sieving with a 80-mesh sieve, adding caustic soda solution with the caustic soda concentration of 1mol/L, ball milling for 2 hours in a ball mill, decomposing organic matters on the surfaces of the oyster shells, and hydrolyzing proteins to obtain wet materials. Cleaning and drying wet materials to obtain fluffy oyster shell powder, then placing the fluffy oyster shell powder in a microwave rapid ashing furnace which is filled with oxygen, carrying out thermal decomposition for 0.5h at 700 ℃, absorbing and releasing impurity gases such as CO 2、NO2、SO2 by using waste caustic soda solution, and obtaining the remainder which is the high-capacity CaO carbon-fixing biological material.|[0046] The specific surface area is measured by a BK122T-B GAWGB aperture adsorption tester and calculated by a BET method, and the carbon fixation capacity is measured by performing a CO 2 absorption and capture experiment on a thermogravimetric analyzer. The specific surface area is measured by a comparison method, a standard sample with known specific surface area is adopted to compare the sample of the adsorbent to be measured in the parallel gas path, the specific surface area value of the adsorbent to be measured can be read out according to the multiple relation of adsorption/regeneration peak values on a computer, and the CaO specific surface area is measured to be 10.54m 2/g. Weighing a certain amount of CaO, placing the CaO in a sample vessel, heating the CaO to 600-650 ℃ in a thermogravimetric analyzer, keeping the temperature for 10min, and introducing CO 2 gas, wherein the weight gain corresponds to the amount of trapped CO 2 because the CaO traps CO 2 and is converted into CaCO 3, and the capacity of the trapped CO 2 is calculated to be 0.442g/g, so that the theoretical adsorption capacity is 56% (the theoretical value of the trapped CO 2 of CaO is 0.789 g/g).|[0047] Example 4|[0048] Crushing the cleaned oyster shells, sieving with a 80-mesh sieve, adding caustic soda solution with the caustic soda concentration of 1mol/L, ball milling for 2 hours in a ball mill, decomposing organic matters on the surfaces of the oyster shells, and hydrolyzing proteins to obtain wet materials. Cleaning and drying wet materials to obtain fluffy oyster shell powder, then placing the fluffy oyster shell powder in a microwave rapid ashing furnace which is filled with oxygen, carrying out thermal decomposition for 1h at 750 ℃, absorbing and releasing impurity gases such as CO 2、NO2、SO2 by using waste caustic soda solution, and obtaining the remainder which is the high-capacity CaO carbon-fixing biological material.|[0049] The specific surface area is measured by a BK122T-B GAWGB aperture adsorption tester and calculated by a BET method, and the carbon fixation capacity is measured by performing a CO 2 absorption and capture experiment on a thermogravimetric analyzer. The specific surface area is measured by a comparison method, a standard sample with known specific surface area is adopted to compare the sample of the adsorbent to be measured in the parallel gas path, the specific surface area value of the adsorbent to be measured can be read out according to the multiple relation of adsorption/regeneration peak values on a computer, and the CaO specific surface area is measured to be 11.87m 2/g. Weighing a certain amount of CaO, placing the CaO in a sample vessel, heating the CaO to 650-700 ℃ in a thermogravimetric analyzer, keeping the temperature for 10min, and introducing CO 2 gas, wherein the weight gain corresponds to the amount of trapped CO 2 because the CaO traps CO 2 and is converted into CaCO 3, and the capacity of the trapped CO 2 is calculated to be 0.497g/g, so that the theoretical adsorption capacity is 63% (the theoretical value of the trapped CaO CO 2 is 0.789 g/g). In this example, the temperature of the pyrolysis gasification was increased as compared with example 3, and the specific surface area and the trapped CO 2 were increased, so that the reaction of CaCO 3 and proteolysis and the like was more complete and the CaO activity was increased by increasing the temperature.|[0050] From examples 1 to 4, it is understood that the oyster shell powder is treated with a caustic soda solution to remove organic matters on the surface of oyster shell and hydrolyze proteins into small molecule products such as amino acids or polypeptides linked with a plurality of amino acids. The oyster shell powder obtained by alkali treatment is decomposed more thoroughly in the thermal decomposition process, and has higher thermal decomposition efficiency. The invention adopts the steps of crushing, mechanochemical ball milling and cleaning and drying, which belong to short-time low-energy-consumption process steps, and the polluted gas generated in the microwave thermal decomposition process is absorbed by the waste alkali liquid treated by the oyster shell powder, thus preventing the pollution to the atmosphere, being environment-friendly, and having simple preparation process, energy conservation and environmental protection. . The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention. (CN118270818)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of biological materials, and particularly relates to a high-capacity carbon-fixing biological material derived from oyster shells and a preparation method thereof.|BACKGROUND ART|[0003] At present, the main way of absorbing carbon dioxide by nature is ocean and forest, the ocean area of the earth occupies 71 percent of the earth surface area, which is 2.4 times of the land area, and the reasonable utilization of ocean resources becomes a huge assistance for realizing double carbon. China is a large country for oyster cultivation, the resources are very rich, the production market is huge, the proportion of oyster shells accounts for 70% -95% of the wet weight of the oysters, and calcium carbonate reaches 90% -99% in the oyster shells. The average amount of calcium carbonate produced by Chinese double-shell aquaculture per year is approximately 800 ten thousand metric tons. Through double-shell aquaculture, a large amount of CO 2 in the seawater is absorbed, the seawater is stored in a CaCO 3 mode, the concentration of carbon dioxide in the seawater is reduced, the absorption of CO 2 in the air by the ocean is further enhanced, and the purpose of carbon fixation is achieved. However, after oysters are eaten, oyster shells are used as byproducts of mariculture oysters, the annual yield is huge, and efficient recycling is urgently needed. Therefore, the oyster shell is comprehensively recycled to produce high added value products, so that good economic benefits can be generated, solid waste resources can be reused, and negative ecological environment influence can be eliminated.|[0004] The CCUS (CO 2 capture, sequestration and utilization technology) can separate CO 2 from industrial processes, energy utilization or the atmosphere for direct utilization, or injection into a formation to achieve permanent sequestration of CO 2, is an important technological option for achieving low-carbon utilization of fossil energy. The invention patent CN202410129929.8 discloses a seawater-based repeated efficient carbon fixing method, which comprises the steps of introducing carbon dioxide-containing gas into seawater, adding a carbon fixing agent for activation when the pH value of the carbon dioxide-containing gas is lower than 6.8, obtaining an alkaline solution containing Ca 2+、Mg2+ ions, and introducing the carbon dioxide-containing gas into the alkaline solution for carbon fixing. The carbon fixing process is based on sea water condition, most occasions cannot utilize the carbon fixing agent, the carbon fixing agent is prepared by uniformly mixing calcined dolomite, magnesium chloride, calcium oxide and calcium chloride, the raw material preparation process is relatively complex, and the carbon fixing process is discontinuous. The patent CN201811351040.5 discloses a semi-closed energy conversion remote transmission and carbon fixation system taking magnesium as a carrier, wherein the carbon fixation process depends on redundant energy sources of renewable energy sources and magnesium produced by an electrolytic magnesium plant, the energy sources are unstable, meanwhile, raw material magnesium can reach a use place only by long-distance transportation, the energy consumption is higher, the carbon fixation system is limited to a larger extent, and the carbon fixation process cannot be continuous. The invention patent CN202311330588.2 discloses a microalgae carbon fixing device and a carbon fixing method, wherein the microalgae periodically supplements a strengthening culture medium into circulating water and introduces mixed gas containing CO 2 in the culture process, so that the microalgae grow at a high speed and have high biomass concentration in an optimal feeding mode, and the microalgae can be used for fixing higher CO 2 in a short time so as to achieve the aim of biological carbon fixing. The method for carbon fixation has higher requirements on microalgae, can be optimized only by meeting various indexes, achieves the aim of carbon fixation, is greatly influenced by factors such as environment, has higher cost, and has a non-concise and continuous carbon fixation process.|[0005] The method for preparing the carbon-fixing biological material by using a large amount of oyster shells generated by oyster cultivation has the advantages of rich and sustainable raw material sources, and the special honeycomb structure of the oyster shells enables the carbon-fixing biological material to have the carbon-fixing characteristics of high specific surface area, high activity and large capacity, so that the method provides technical guarantee for the value-added utilization of the oyster shells and the mass production of the carbon-fixing biological material.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to provide a high-capacity carbon-fixing biological material derived from oyster shells and a preparation method thereof. The method is characterized in that a byproduct oyster shell of sea water oyster cultivation is used as a raw material, and the high-capacity carbon-fixing biological material with high activity and high specific surface area is prepared through the process steps of mixing oyster shell powder obtained by crushing oyster shells with caustic soda solution, ball milling by a mechanochemical method, cleaning and drying wet materials, microwave thermal decomposition and the like. The preparation method has the advantages of abundant raw material sources, low cost, simple preparation process flow, energy conservation and environmental protection, prepares the high-capacity carbon-fixing biological material, realizes the recycling of solid waste resources, can be used for absorbing carbon dioxide in the atmosphere, achieves the purpose of carbon fixing, has good economic and ecological benefits, and has important significance for realizing the double-carbon target and the sustainable development of the whole society.|[0007] The oyster powder is added into caustic soda solution for mechanochemical treatment, so that the oyster powder can catalyze and hydrolyze organic proteins in oyster shells and decompose the organic proteins into small molecular weight proteins or polypeptides linked by a plurality of amino acids. After the protein in the oyster shell is hydrolyzed, the adhesiveness among calcium carbonate particles in the oyster shell is greatly reduced, and the oyster shell powder obtained by washing and drying is fluffier, so that the oyster shell powder has the characteristics of higher specific surface area, high activity and the like while retaining a honeycomb structure. By adopting microwave heat treatment, the heating efficiency is greatly improved, the simultaneous heating of the inside and the outside of the oyster shell powder can be ensured, collapse caused by uneven heating of the structure is avoided, the specific surface area and the activity are reduced, and the carbon fixing capability of the product is ensured to the greatest extent. In the microwave thermal decomposition stage, chemical reactions such as thermal decomposition of calcium carbonate and hydrolyzed protein, treatment of waste gas generated by thermal decomposition and the like are performed, so that the tail gas is prevented from being discharged into the atmosphere to pollute the environment.|[0008] (1) Calcium carbonate decomposition reaction|[0009] |[0010] (2) Protein decomposition reaction|[0011] |[0012] (3) C, N, S oxide tail gas treatment|[0013] CO2+2NaOH→Na2CO3+H2O|[0014] 2NO2+2NaOH→NaNO3+NaNO2+H2O|[0015] SO2+2NaOH→Na2SO3+H2O|[0016] The invention provides a preparation method of a high-capacity carbon-fixing biological material derived from oyster shells, which comprises the following steps:|[0017] Step S1: preparing oyster shell into oyster shell powder; |[0018] Step S2: adding caustic soda solution into oyster shell powder, ball milling in a ball mill, and uniformly mixing to obtain wet materials; |[0019] step S3: washing and drying the wet material to obtain dried and fluffy oyster shells; |[0020] Step S4: placing the fluffy oyster shell powder in a microwave rapid ashing furnace, and carrying out thermal decomposition at a certain temperature in an oxygen atmosphere to release carbon, nitrogen and sulfur oxide gases to obtain a carbon-fixing biological material; |[0021] further, in the step S1, the particle size of the oyster shell powder is 40-80 mesh screen; |[0022] further, in the step S2, the concentration of the caustic soda solution is 0.1-1 mol/L, and the ball milling time is 0.5-2 h; |[0023] further, in the step S4, the thermal decomposition temperature of the oyster shell powder is 600-800 ℃ and the thermal decomposition time is 0.1-1 h; |[0024] Further, the caustic soda solution used in step S2 may be used to absorb the tail gas in step S4, and perform the tail gas treatment to prevent air pollution. |[0025] The invention has the beneficial effects that:|[0026] (1) The invention uses oyster shell waste with high yield and not effectively utilized as raw materials, has rich sources of raw materials, not only recycles solid waste resources, but also generates certain economic benefit, and improves the civil and environmental problems. |[0027] (2) The invention uses caustic soda solution to hydrolyze protein in oyster shell into micromolecular protein or polypeptide, reduces the adhesiveness between calcium carbonate particles, is convenient for complete thermal decomposition of calcium carbonate and organic matters in the micro-blog thermal decomposition stage, and the obtained CaO carbon-fixing biological material has higher specific surface area and activity.|[0028] (3) The ball milling and microwave thermal decomposition of the invention belongs to short-time low-energy-consumption process steps, oxygen is introduced during thermal decomposition, so as to ensure the complete decomposition of calcium carbonate, protein and the like, and the oyster powder alkali treatment solution is utilized to absorb waste gas generated by the microwave thermal decomposition, thereby preventing tail gas from polluting air.|[0029] (4) The invention adopts a microwave rapid ashing furnace to thermally decompose oyster shell powder treated by caustic soda solution, and microwave heating belongs to an internal heat source method, so that the temperature rising speed is high, the oyster shell powder is uniformly heated as a whole, the high specific surface area of the oyster shell powder is reserved, the high activity of the oyster shell powder is maintained, and the thermal decomposition efficiency is high.|DRAWINGS DESCRIPTION|[0030] FIG. 1 is a process flow of preparing a high-capacity carbon-fixing biomaterial derived from oyster shells.|INVENTION MODE|Detailed Description|[0031] In order that the above-recited objects, features and advantages of the invention will be more clearly understood, a more particular description of the invention will be rendered by reference to specific embodiments thereof. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways than those described herein, and therefore the present invention is not limited to the specific embodiments disclosed below.|[0032] Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this application pertains. The terms "first," "second," and the like in the description and in the claims, are not used for any order, quantity, or importance, but are used for distinguishing between different elements. Likewise, the terms "a" or "an" and the like do not denote a limitation of quantity, but rather denote the presence of at least one.|[0033] As shown in fig. 1, a preparation method of a high-capacity carbon-fixing biological material derived from oyster shells comprises the following steps:|[0034] step S1: preparing oyster shell into oyster shell powder, and sieving with a 40-80 mesh sieve; |[0035] step S2: adding caustic soda solution into oyster shell powder, ball milling in a ball mill, and uniformly mixing to obtain wet materials, wherein the concentration of the caustic soda is 0.1 mol/L-1 mol/L, and the ball milling time is 0.5-2 h; |[0036] step S3: washing and drying the wet material to obtain dried and fluffy oyster shell powder; |[0037] step S4: placing the fluffy oyster shell powder in a microwave rapid ashing furnace, carrying out thermal decomposition at a certain temperature in an oxygen atmosphere to release carbon, nitrogen and sulfur oxide gases, wherein the remainder is a carbon-fixing biological material, the thermal decomposition temperature of the oyster shell powder is 600-800 ℃, the thermal decomposition time is 0.1-1 h, and the released tail gas is absorbed by waste alkali liquor in the step S2; |[0038] Example 1 |[0039] Crushing the cleaned oyster shells, ball-milling the crushed oyster shells in a ball mill for 1h through a 40-mesh screen, cleaning and drying the obtained material to obtain fluffy oyster shell powder, then placing the fluffy oyster shell powder in a microwave rapid ashing furnace which is introduced with oxygen atmosphere, carrying out thermal decomposition for 0.1h at 600 ℃, absorbing and releasing impurity gases such as CO 2、NO2、SO2 by using waste caustic soda solution, and obtaining the remainder which is the high-capacity CaO carbon-fixing biological material.|[0040] The specific surface area is measured by a BK122T-B GAWGB aperture adsorption tester and calculated by a BET method, and the carbon fixation capacity is measured by performing a CO 2 absorption and capture experiment on a thermogravimetric analyzer. The specific surface area is measured by a comparison method, a standard sample with known specific surface area is adopted to compare the sample of the adsorbent to be measured in the parallel gas path, the specific surface area value of the adsorbent to be measured can be read out according to the multiple relation of adsorption/regeneration peak values on a computer, and the CaO specific surface area is measured to be 3.13m 2/g. Weighing a certain amount of CaO, placing the CaO in a sample vessel, heating the CaO to 600-650 ℃ in a thermogravimetric analyzer, keeping the temperature for 10min, and introducing CO 2 gas, wherein the weight gain corresponds to the amount of trapped CO 2 because the CaO traps CO 2 and is converted into CaCO 3, and the capacity of the trapped CO 2 is calculated to be 0.209g/g, so that the theoretical adsorption capacity is 26% (the theoretical value of the trapped CO 2 of CaO is 0.789 g/g).|[0041] Example 2|[0042] Crushing the cleaned oyster shells, sieving with a 40-mesh sieve, adding caustic soda solution with caustic soda concentration of 0.5mol/L, ball milling for 2 hours in a ball mill, decomposing organic matters on the surfaces of the oyster shells, and hydrolyzing proteins to obtain wet materials. Cleaning and drying wet materials to obtain fluffy oyster shell powder, then placing the fluffy oyster shell powder in a microwave rapid ashing furnace which is filled with oxygen, carrying out thermal decomposition for 0.3h at 650 ℃, absorbing and releasing impurity gases such as CO 2、NO2、SO2 by using waste caustic soda solution, and obtaining the remainder which is the high-capacity CaO carbon-fixing biological material.|[0043] The specific surface area is measured by a BK122T-B GAWGB aperture adsorption tester and calculated by a BET method, and the carbon fixation capacity is measured by performing a CO 2 absorption and capture experiment on a thermogravimetric analyzer. The specific surface area is measured by a comparison method, a standard sample with known specific surface area is adopted to compare the sample of the adsorbent to be measured in a parallel gas path, the specific surface area value of the adsorbent to be measured can be read out according to the multiple relation of adsorption/regeneration peak values on a computer, and the CaO specific surface area is measured to be 9.24m 2/g. Weighing a certain amount of CaO, placing the CaO in a sample vessel, heating the CaO to 600-650 ℃ in a thermogravimetric analyzer, keeping the temperature for 10min, and introducing CO 2 gas, wherein the weight gain corresponds to the amount of trapped CO 2 because the CaO traps CO 2 and is converted into CaCO 3, and calculating the capacity of trapped CO 2 to reach 48% of theoretical adsorption capacity (the theoretical value of the trapped CaO CO 2 is 0.789 g/g).|[0044] Example 3|[0045] Crushing the cleaned oyster shells, sieving with a 80-mesh sieve, adding caustic soda solution with the caustic soda concentration of 1mol/L, ball milling for 2 hours in a ball mill, decomposing organic matters on the surfaces of the oyster shells, and hydrolyzing proteins to obtain wet materials. Cleaning and drying wet materials to obtain fluffy oyster shell powder, then placing the fluffy oyster shell powder in a microwave rapid ashing furnace which is filled with oxygen, carrying out thermal decomposition for 0.5h at 700 ℃, absorbing and releasing impurity gases such as CO 2、NO2、SO2 by using waste caustic soda solution, and obtaining the remainder which is the high-capacity CaO carbon-fixing biological material.|[0046] The specific surface area is measured by a BK122T-B GAWGB aperture adsorption tester and calculated by a BET method, and the carbon fixation capacity is measured by performing a CO 2 absorption and capture experiment on a thermogravimetric analyzer. The specific surface area is measured by a comparison method, a standard sample with known specific surface area is adopted to compare the sample of the adsorbent to be measured in the parallel gas path, the specific surface area value of the adsorbent to be measured can be read out according to the multiple relation of adsorption/regeneration peak values on a computer, and the CaO specific surface area is measured to be 10.54m 2/g. Weighing a certain amount of CaO, placing the CaO in a sample vessel, heating the CaO to 600-650 ℃ in a thermogravimetric analyzer, keeping the temperature for 10min, and introducing CO 2 gas, wherein the weight gain corresponds to the amount of trapped CO 2 because the CaO traps CO 2 and is converted into CaCO 3, and the capacity of the trapped CO 2 is calculated to be 0.442g/g, so that the theoretical adsorption capacity is 56% (the theoretical value of the trapped CO 2 of CaO is 0.789 g/g).|[0047] Example 4|[0048] Crushing the cleaned oyster shells, sieving with a 80-mesh sieve, adding caustic soda solution with the caustic soda concentration of 1mol/L, ball milling for 2 hours in a ball mill, decomposing organic matters on the surfaces of the oyster shells, and hydrolyzing proteins to obtain wet materials. Cleaning and drying wet materials to obtain fluffy oyster shell powder, then placing the fluffy oyster shell powder in a microwave rapid ashing furnace which is filled with oxygen, carrying out thermal decomposition for 1h at 750 ℃, absorbing and releasing impurity gases such as CO 2、NO2、SO2 by using waste caustic soda solution, and obtaining the remainder which is the high-capacity CaO carbon-fixing biological material.|[0049] The specific surface area is measured by a BK122T-B GAWGB aperture adsorption tester and calculated by a BET method, and the carbon fixation capacity is measured by performing a CO 2 absorption and capture experiment on a thermogravimetric analyzer. The specific surface area is measured by a comparison method, a standard sample with known specific surface area is adopted to compare the sample of the adsorbent to be measured in the parallel gas path, the specific surface area value of the adsorbent to be measured can be read out according to the multiple relation of adsorption/regeneration peak values on a computer, and the CaO specific surface area is measured to be 11.87m 2/g. Weighing a certain amount of CaO, placing the CaO in a sample vessel, heating the CaO to 650-700 ℃ in a thermogravimetric analyzer, keeping the temperature for 10min, and introducing CO 2 gas, wherein the weight gain corresponds to the amount of trapped CO 2 because the CaO traps CO 2 and is converted into CaCO 3, and the capacity of the trapped CO 2 is calculated to be 0.497g/g, so that the theoretical adsorption capacity is 63% (the theoretical value of the trapped CaO CO 2 is 0.789 g/g). In this example, the temperature of the pyrolysis gasification was increased as compared with example 3, and the specific surface area and the trapped CO 2 were increased, so that the reaction of CaCO 3 and proteolysis and the like was more complete and the CaO activity was increased by increasing the temperature.|[0050] From examples 1 to 4, it is understood that the oyster shell powder is treated with a caustic soda solution to remove organic matters on the surface of oyster shell and hydrolyze proteins into small molecule products such as amino acids or polypeptides linked with a plurality of amino acids. The oyster shell powder obtained by alkali treatment is decomposed more thoroughly in the thermal decomposition process, and has higher thermal decomposition efficiency. The invention adopts the steps of crushing, mechanochemical ball milling and cleaning and drying, which belong to short-time low-energy-consumption process steps, and the polluted gas generated in the microwave thermal decomposition process is absorbed by the waste alkali liquid treated by the oyster shell powder, thus preventing the pollution to the atmosphere, being environment-friendly, and having simple preparation process, energy conservation and environmental protection. . The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention. Family Number|(110457368)|110457368|Abstract|(CN118270818 A)|The invention relates to a high - capacity carbon sequestration biological material derived from oyster shells and a preparation method of the high - capacity carbon sequestration biological material , and belongs to the field of biological materials . The preparation method comprises the following steps : by taking a byproduct oyster shell of mariculture oysters as a raw material , crushing the oyster shell to obtain oyster shell powder , mixing the oyster shell powder with a caustic soda aqueous solution , performing mechanochemical treatment in a ball mill , cleaning and drying a wet material , and performing microwave thermal decomposition in a microwave rapid ashing furnace to prepare the high - capacity carbon sequestration biological material with high activity and high specific surface area . The high - capacity carbon sequestration biological material is rich in raw material source , low in cost , simple in preparation process flow , energy - saving and environment - friendly , not only realizes resource utilization of the oyster shell waste residues , but also is high in carbon sequestration capacity , has remarkable economic and ecological benefits , and is suitable for industrial production . The method has important practical significance on sustainable development and green low - carbon economy of the oyster breeding industry . |CPC codes|(CN118270818 A)|B01D - 053/50/2 |B01D - 053/56 |B01D - 053/60 |B01D - 053/62 |B01D - 053/78 |B01D - 053/81 |B01D - 2251/304 |B01D - 2251/404 |B01D - 2251/602 |B01D - 2251/604 |C01F - 011/06 |C01P - 2006/12 |IPC codes|(CN118270818 A)|B01D - 053/50 |B01D - 053/56 |B01D - 053/60 |B01D - 053/62 |B01D - 053/78 |B01D - 053/81 |C01F - 011/06 |Title|(CN118270818 A)|High - capacity carbon sequestration biological material derived from oyster shells and preparation method of high - capacity carbon sequestration biological material | Environmental technology|Materials, metallurgy B01D-053/50/2|B01D-053/56|B01D-053/60|B01D-053/62|B01D-053/78|B01D-053/81|B01D-2251/304|B01D-2251/404|B01D-2251/602|B01D-2251/604|C01F-011/06|C01P-2006/12|C04B-002/10 B01D-053/50/2|B01D-053/56|B01D-053/60|B01D-053/62|B01D-053/78|B01D-053/81|B01D-2251/304|B01D-2251/404|B01D-2251/602|B01D-2251/604|C01F-011/06|C01P-2006/12|C04B-002/10 B01D-053/50|B01D-053/56|B01D-053/60|B01D-053/62|B01D-053/78|B01D-053/81|C01F-011/06|C04B-002/10 B01D-053/50|B01D-053/56|B01D-053/60|B01D-053/62|B01D-053/78|B01D-053/81|C01F-011/06|C04B-002/10 CN120609724 CN120609724 115930879 WHO=Examiner SELF=N CAT=A PENDING (CN118270818)|PENDING ALIVE (CN118270818)|ALIVE (CN118270818)|LEGAL DETAILS FOR CN118270818|Actual or expected expiration date=2044-03-29|Legal state=ALIVE|Status=PENDING|Event publication date=2024-03-29|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202410375034|Application date=2024-03-29|Standardized application number=2024CN-0375034|Event publication date=2024-07-02|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN118270818|Publication stage code=A|Publication date=2024-07-02|Standardized publication number=CN118270818|Event publication date=2024-07-02|Event code=CN/PB01|Event group=Examination events|Publication (CN118270818)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQyp+jEz4XPA1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073392540&ekey=2013&xpn=CN118270818&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=wp9V70vDLn6vVQaWC3rBe5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN118270818)|CN (CN118270818)|NAME=NANCHANG HANGKONG UNIVERSITY , COUNTRY=CN (CN118270818)|NAME=LIU AIFANG;NANCHANG QINGYUAN PATENT AGENT OFFICE (GENERAL PARTNERSHIP) , REG=36123 (CN118270818)|NAME=LU JINSHAN|NAME=WU JINAN|NAME=SHU JIAXIN|NAME=WANG FANGQIANG 0 1 Titre: (CN118270818)|High-capacity carbon sequestration biological material derived from oyster shells and preparation method of high-capacity carbon sequestration biological material Résumé: (CN118270818)|The invention relates to a high-capacity carbon sequestration biological material derived from oyster shells and a preparation method of the high-capacity carbon sequestration biological material, and belongs to the field of biological materials. The preparation method comprises the following steps: by taking a byproduct oyster shell of mariculture oysters as a raw material, crushing the oyster shell to obtain oyster shell powder, mixing the oyster shell powder with a caustic soda aqueous solution, performing mechanochemical treatment in a ball mill, cleaning and drying a wet material, and performing microwave thermal decomposition in a microwave rapid ashing furnace to prepare the high-capacity carbon sequestration biological material with high activity and high specific surface area. The high-capacity carbon sequestration biological material is rich in raw material source, low in cost, simple in preparation process flow, energy-saving and environment-friendly, not only realizes resource utilization of the oyster shell waste residues, but also is high in carbon sequestration capacity, has remarkable economic and ecological benefits, and is suitable for industrial production. The method has important practical significance on sustainable development and green low-carbon economy of the oyster breeding industry. 8 Abstract gpt-4o-mini no The article focuses on a carbon sequestration material derived from oyster shells, which does not involve the accelerated weathering of silicate or alkaline minerals for CO₂ capture.
12 US63/213,398|US63/213,398P|US63/289,395|US63/289,395P|EP22829238|US17/846,838|US63/322,672|US63/322,672P|WOUS2022/034546|US18/128,583|US18/435,492|US19/335,929 US19/335,929|US18/435,492|HK42023083673|US18/128,583|WOUS2022/034546|HK62023083672|BR112023023226|EP22829238|EP23199092|AU2022299180|CA3207124|US17/846,838 US20260016458|BR112023023226|EP4256520|EP4256520|US12422425|EP4256520|AU2022299180|US20240264139|EP4276752|US11921098|BR112023023226|HK40094979|HK40095252|EP4276752|BR112023023226|EP4256520|US20230273174|AU2022299180|US11644454|CA3207124|WO2022/271842|US20220404329 103013820 US20260016458 A1 2026-01-15 [US20260016458]|US12422425 B2 2025-09-23 [US12422425]|US20240264139 A1 2024-08-08 [US20240264139]|HK40094979 A 2024-01-26 [HK40094979]|US11921098 B2 2024-03-05 [US11921098]|US20230273174 A1 2023-08-31 [US20230273174]|WO2022/271842 A1 2022-12-29 [WO2022271842]|HK40095252 A 2024-01-26 [HK40095252]|BR112023023226 B1 2026-01-13 [BR112023023226]|BR112023023226 A2 2024-01-30 [BR112023023226]|BR112023023226 A0 2023-11-14 [BR112023023226]|EP4256520 B1 2025-12-10 [EP4256520]|EP4256520 C0 2025-12-10 [EP4256520]|EP4256520 A4 2024-11-06 [EP4256520]|EP4256520 A1 2023-10-11 [EP4256520]|EP4276752 A3 2024-07-17 [EP4276752]|EP4276752 A2 2023-11-15 [EP4276752]|AU2022299180 A9 2024-10-24 [AU2022299180]|AU2022299180 A1 2023-07-13 [AU2022299180]|CA3207124 A1 2022-12-29 [CA3207124]|US11644454 B2 2023-05-09 [US11644454]|US20220404329 A1 2022-12-22 [US20220404329] 2021-06-22|2021-12-14|2022-03-23|2022-06-22|2023-03-30|2024-02-07|2025-09-22 2025-09-22|2024-02-07|2023-12-05|2023-03-30|2022-06-22|2023-12-05|2022-06-22|2022-06-22|2022-06-22|2022-06-22|2022-06-22|2022-06-22 2026-01-15|2026-01-13|2025-12-10|2025-12-10|2025-09-23|2024-11-06|2024-10-24|2024-08-08|2024-07-17|2024-03-05|2024-01-30|2024-01-26|2024-01-26|2023-11-15|2023-11-14|2023-10-11|2023-08-31|2023-07-13|2023-05-09|2022-12-29|2022-12-29|2022-12-22 (EP4256520)|2025-12-10||(US12422425)|2025-09-23|(US11921098)|2024-03-05|(US11644454)|2023-05-09|||(BR112023023226)|2026-01-13|||| (EP4256520)|2042-06-22|(EP4276752)|2042-06-22|(US12422425)|2042-06-22|(US11921098)|2042-06-22|(US11644454)|2042-06-22|(US20260016458)|2042-06-22|(WO2022/271842)|2024-12-22|(BR112023023226)|2042-06-22|(AU2022299180)|2042-06-22|(HK40095252)|2042-06-22|(HK40094979)|2043-12-05|(CA3207124)|2042-06-22 (EP4256520)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering (EP4256520)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering. EION (EP4256520)|Eion Corp.|(EP4256520)|Eion Corp. ([US])|(EP4256520)|Eion Corp.|(EP4256520)|Eion Corp. ([US])|(EP4276752)|Eion Corp. ([US])|(EP4276752)|Eion Corp. ([US])|(US12422425)|Eion Corp. ([US])|(US20240264139)|Eion Corp. ([US])|(US11921098)|Eion Corp. ([US])|(US20230273174)|Eion Corp. ([US])|(US11644454)|Eion Corp. ([US])|(US20220404329)|Eion Corp. ([US])|(US20260016458)|Eion Corp. ([US])|(WO2022/271842)|EION CORP. ([US])|(BR112023023226)|CORP EION ([US])|(BR112023023226)|CORP EION ([US])||(AU2022299180)|EION CORP.|(AU2022299180)|EION CORP.|(HK40095252)|Eion Corp ([US])|(HK40094979)|Eion Corp ([US])|(CA3207124)|EION CORP. ([US]) WOLF ADAM|CHANG ELLIOT SUK-HYUN|TANK ALAN ROBERT (EP4256520)|WOLF, Adam|CHANG, Elliot Suk-Hyun|TANK, Alan Robert|(EP4256520)|WOLF, Adam|CHANG, Elliot Suk-Hyun|TANK, Alan Robert|(EP4256520)|WOLF, Adam|CHANG, Elliot Suk-Hyun|TANK, Alan Robert|(EP4256520)|WOLF, Adam|CHANG, Elliot Suk-Hyun|TANK, Alan Robert (EP4256520)|Dragotti & Associati S.P.A. ([IT])|Reg. Nb: 101869514|(EP4276752)|Dragotti & Associati S.R.L. ([IT])|Reg. Nb: 101869514|(US12422425)|Frost Brown Todd LLP|VanDrake, III Vance V.|Johnson Alexander J.|(US11921098)|Frost Brown Todd LLP|VanDrake, III Vance V.|Johnson Alexander J.|(US11644454)|Ulmer & Berne LLP|Van Drake, III Vance V.|Johnson Alexander J.|(WO2022/271842)|FALK, Daniel T. et al. ([US])|(AU2022299180)|AJ Pietras IP Limited ([NZ])|(HK40095252)|HNC INNOVATION LIMITED ([HK])|(HK40094979)|HNC INNOVATION LIMITED ([HK])|(CA3207124)|BURNET, DUCKWORTH & PALMER LLP ([CA]) (EP4256520)|This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).|VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.|Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.|The potential for ERW as a commercial enterprise is limited by some fundamental issues:| (EP4256520)|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring the immobile trace elements in a soil sample after application of the mineral amendment to verify application of the mineral amendment, characterized in that the method comprises the steps of: determining the amount of the mineral amendment added to the soil sample, determining the amount of measured divalent cations in the soil sample, determining the fractional carbon dioxide removal by comparing the applied divalent cations to the measured divalent cations in the soil sample.| (EP4276752)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.| (EP4276752)|ENHANCED ROCK(100,2)|MINERAL AMENDMENT(100,2)|REMOVING CARBON(100,1)|VERIFICATION(100,1)|ENHANCED ROCK WEATHERING(82,1)|IMMOBILE TRACE ELEMENT(35,1)||(EP4276752)|ENHANCED ROCK(100,2)|MINERAL AMENDMENT(100,2)|REMOVING CARBON(100,1)|VERIFICATION(100,1)|ENHANCED ROCK WEATHERING(82,1)|IMMOBILE TRACE ELEMENT(35,1)||(US12422425)|MINERAL AMENDMENT(100,22)|VERIFICATION(100,17)|REMOVING CARBON(100,12)|ENHANCED ROCK(100,8)|COMMINUTED SILICATE MINERAL(68,3)|SILICATE MINERAL AGGLOMERATION(52,2)|ENHANCED ROCK WEATHERING(46,2)|INTERESTED PARTY(45,1)|RECOVERING SAMPLING COLUMN(38,1)|FUNDAMENTAL ISSUE(37,1)|CARBON MEASUREMENT OBJECTIVE(25,1)|LANDOWNER(23,1)|SLOW RELEASE ACIDIFIER(22,3)|IMMOBILE TRACE ELEMENT(21,25)|COMMERCIAL ENTERPRISE(17,1)|GIBBSITE(15,2)|BINDER(14,3)|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)|NEODYMIUM(12,11)|BRUKER PROPRIETARY GEO CALIBRATION(12,1)|VANADIUM(12,1)|EUROPIUM(11,10)|DYSPROSIUM(11,9)|LANTHANUM(11,9)|SAMARIUM(11,8)|SCANDIUM(11,8)|YTTERBIUM(11,8)|GADOLINIUM(11,7)|PRASEODYMIUM(11,6)|BERYLLIUM(11,2)|GERMANIUM(11,2)|RUBIDIUM(11,2)|ZIRCONIUM(11,2)|HOLMIUM(10,6)|LUTETIUM(10,6)|THULIUM(10,6)|DRAWDOWN CALCULATION(10,4)|ANDTHE TRANSITION METAL(10,1)|AVERAGE PARTICLE SIZE(9,4)|ERW(9,4)|BLAST FURNACE SLAG(9,2)|CESIUM(9,2)|CHROMIUM(9,2)|GALLIUM(9,2)|HAFNIUM(9,2)|NIOBIUM(9,2)|RIGOROUS QUANTIFICATION(9,2)|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)|TANTALUM(9,2)|BIOLOGICAL DERIVED COMPONENT(9,1)|PELLETIZED MINERAL AMENDMENT(9,1)|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)|CERIUM(8,9)|YTTRIUM(8,8)|RARE METAL(8,4)|GYPSUM(8,3)|MINERAL SOIL AMENDMENT(8,3)|AIRTIGHT CONTAINMENT(8,2)|NONLIMITING CANDIDATE(8,2)|DELIVER PROSPECTIVE REWARD(8,1)|NEGATIVELY CHARGED BICARBONATE HCO(8,1)|STERILIZED SOIL BEAKER(8,1)|TRANSITION METAL(7,5)|PPB DETECTION(7,4)|INSTRUMENTAL ERROR(7,3)|DISSOLUTION KINETICS(7,2)|PHOSPHATE FERTILIZER(7,2)|PULVERIZED SILICATE(7,2)|ALKALIZER KINETICS(7,1)|MINERAL ADDITIVE PROVEN IDENTITY(7,1)|SOIL ORGANIC CARBON(7,1)|TAXONOMY DISTINGUISHE(7,1)|UNINHABITABLE WATERWAY(7,1)|WET BIOMASS WET ALIQUOT(7,1)|CARBON FLUX(6,3)|CHARGE IMBALANCE(6,2)|INORGANIC ADDITIVE(6,2)|MG PPM DETECTION(6,2)|NEUTRAL GROUND(6,2)|ROCK PARTICLE(6,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)|AGGREGATED PELLET(6,1)|AGLIME SUBSTITUTE(6,1)|AGRICULTURAL SOILS(6,1)|AGRONOMIC PERFORMANCE EXPECTATION(6,1)|ALKALINITY EXPORT(6,1)|BIODEGRADABLE TRANSPORTER(6,1)|BIOFILM MEDIATING(6,1)|CUMULATIVE CATION FLUX MEASURE(6,1)|DDIC DTA ESTIMATE(6,1)|FORSTERITE METRIC TON(6,1)|FORSTERITE TENDENCY(6,1)|HENRY LAW COEFFICIENT(6,1)|INFERRED ION FLUX(6,1)|INSTRUMENTAL UNCERTAINTY(6,1)|INTENSE SCRUTINY(6,1)|MARKETING COLLATERAL(6,1)|MICRONUTRIENT INCORPORATION(6,1)|MYCORRHIZAL INOCULUM(6,1)|NONPROFIT ORGANIZATION(6,1)|OCEAN ACIDIFICATION(6,1)|PELLET AGGLOMERATION(6,1)|PHOSPHORUS ECOSYSTEM LOSS(6,1)|PORTABLE XRF INSTRUMENT(6,1)|PREAPPLICATION SOIL(6,1)|PROTONATED MICROBE(6,1)|PULVERIZED LIMESTONE(6,1)|RENOWNED CHEMIST(6,1)|RESPIRATORY HEALTH IMPACT(6,1)|REWET BIOMASS(6,1)|RIGOROUS COMPLIANCE(6,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)|SOIL CULTIVATED ZONE(6,1)|SOIL GEOCHEMISTRY(6,1)|SOIL HYDROLOGY(6,1)|NACL SOLUTION(5,4)|PROMETHIUM(5,4)|PULVERIZATION(5,4)|TRIPLICATE(5,4)|CENTRIFUGE CELL(5,3)|GROWING PLANT(5,2)|AEROSOL SIZED PARTICLE(5,1)|AGGREGATING GROUND MINERAL(5,1)|ANALYTICAL LABORATORY(5,1)|ANCIENT ROCK FORMATION(5,1)|ANION CONSERVATION(5,1)|CATEGORY REGULATION(5,1)|CATION CONSERVATION(5,1)|CLAUSE XII(5,1)|DISSOLVE ALGINATE(5,1)|DISSOLVED ALGINATE POWDER(5,1)|DOWNSTREAM ECOSYSTEM(5,1)|DOWNSTREAM WATERWAY(5,1)|DTA DH INVERSE(5,1)|DUST PREVALENCE(5,1)|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)|FUNGAL ADJUVANT(5,1)|GROUND MINERAL AGGREGATION(5,1)|KEY INSIGHT(5,1)|MICROBIAL CATION EXCHANGER(5,1)|MINERAL ADJUVANT(5,1)|MINERAL TON HECTARE(5,1)|NUTRIENT AVAILABILITY(5,1)|PELLET DISSOLUTION(5,1)|PHOSPHATE ZINC PRECIPITATE(5,1)|PROGRESS FRACTIONATION(5,1)|QUASI GOVERNMENTAL REGULATOR(5,1)|RESERVOIR GEOLOGY(5,1)|SOIL STERILIZATION(5,1)|SPECIALIZED TOOL(5,1)|STEAM STERILIZATION(5,1)|TECHNO ECONOMIC MODELING(5,1)|ULTIMATE PRICE(5,1)|UREY REACTION BASIC PREMISE(5,1)|V MONTE CARLO SIMULATION(5,1)|VERIFICATION VERSION(5,1)|VERIFIED ENHANCED ROCK(5,1)|VOLUNTARY MARKET(5,1)|RARE EARTH ELEMENT(4,18)|AVOIDED EMISSION(4,2)|CARBONATE SPECIES(4,2)|DISSOLVED CARBONATE(4,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)|MARKET ABILITY(4,2)|MINERAL POTENTIAL(4,2)|SECURE VESSEL(4,2)|SOIL ENVIRONMENT(4,2)|ABUNDANT CO2(4,1)|ACCELERATE TIMING(4,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)|AQUEOUS BICARBONATE MEASUREMENT(4,1)|AQUEOUS COMPLEXATION(4,1)|ASBESTOS EXPOSURE(4,1)|ASSEMBLING MP(4,1)|ATTENDANT DEMAND(4,1)|AUXILIARY GEOCHEMICAL DATA(4,1)|BICARBONATE MOLE(4,1)|BROAD FRAMEWORK(4,1)|CARBON EXCHANGE TRANSACTION(4,1)|CARBON VERIFICATION BENEFIT(4,1)|COARSE PARTICLE(4,1)|COLLECT CELL PELLET(4,1)|CONTINENTAL COLLISION RELEASE(4,1)|CROP HEALTH(4,1)|DISSOLUTION ENHANCING(4,1)|DIVALENT MG(4,1)|EQUILIBRIUM EQUATION(4,1)|FERTILIZATION FREQUENCY(4,1)|FRAUDULENT SAMPLE(4,1)|GROUND NATURAL ENVIRONMENT(4,1)|INCREASE ECOSYSTEM COBENEFIT(4,1)|LB BROTH(4,1)|MINERAL TRANSFORMATION EXTENT(4,1)|MINUS PROTON DONOR(4,1)|PHOSPHATE LEACHING(4,1)|PHOSPHATE MOBILITY(4,1)|PRECISE ANSWER(4,1)|PREEQUILIBRATED TUBE(4,1)|PULVERIZED MG(4,1)|REACTION THERMODYNAMICS(4,1)|SECURITIZED CARBON REMOVAL(4,1)|SILICATE MINERAL SHELL(4,1)|SILICATE ROLE(4,1)|UNSEALING SAMPLE(4,1)|VERIFIABLE CARBON REMOVAL(4,1)|XRF ANALYSIS(4,1)|K2H(3,4)|BAG(3,2)|COMMINUTION(3,2)|FARMER(3,2)|PELLETIZING(3,2)|PRODUCT FORMULATION(3,2)|STAKEHOLDER(3,2)|TOTAL FORMULATION(3,2)|ACIDIC ENVIRONMENT(3,1)|ANALYTICAL PERFORMANCE(3,1)|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)|CARBON MARKET MATURATION(3,1)|CARBON REMOVAL VERIFICATION(3,1)|CARBON TRANSACTION(3,1)|COMPUTING INDEX(3,1)|CORTEVA CARBON(3,1)|DRIED PELLET(3,1)|EMPLACEMENT LOCATION(3,1)|ENTIRE US ECONOMY(3,1)|EXCHANGE COEFFICIENT(3,1)|EXCHANGING RESIN(3,1)|EXPERIMENTAL WORK(3,1)|EXTANT FARM EQUIPMENT(3,1)|FILTRATE ANALYSIS(3,1)|FULL SUMMATION(3,1)|GRIND CELL(3,1)|HEAVY PHOSPHATE(3,1)|ICP ANALYSIS(3,1)|IMMOBILIZATION(3,1)|INDIGO CARBON(3,1)|LABORATORY SETTING(3,1)|MARINE SETTING(3,1)|MINERAL DELIVERY(3,1)|MINERAL DISSOLUTION RATE(3,1)|NATURAL ABUNDANCE CALCULATION(3,1)|NATURAL SOILS(3,1)|NEGATIVE EMISSION(3,1)|PLANT DEMAND(3,1)|PROJECT EVALUATION CRITERIA(3,1)|RELEVANT ION(3,1)|ROCK ELEMENTAL ANALYSIS(3,1)|ROCK MATERIAL ACCELERATED WEATHERING(3,1)|SAMPLING DENSITY(3,1)|SHARP THRESHOLD(3,1)|SOIL ELEMENTAL ANALYSIS(3,1)|SUBSURFACE SOIL PORE WATER(3,1)|TECHNOLOGICAL SOLUTION(3,1)|WET GRAM(3,1)|T N(2,9)|ANALYTICAL CHEMISTRY(2,3)|K1H(2,3)|LYSE(2,3)|SOIL SAMPLE(2,3)|ABILITY THRESHOLD(2,1)|ACCEPTANCE(2,1)|ACCOUNTING(2,1)|ACID TREATED ARTHROBACTER(2,1)|ACIDIC SOIL SOLUTION(2,1)|ADDITIONALITY(2,1)|ADMIXTURE(2,1)|AERATION(2,1)|AGLIME MESH SIZE OBSERVATION(2,1)|AGRICULTURE(2,1)|ALGAL BLOOM(2,1)|ANALYTICAL SOLUTION(2,1)|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)|ATTRACTION(2,1)|AUTOCLAVE(2,1)|BACTERIA(2,1)|BIOADSORBED METAL ACTIVE RELEASE(2,1)|BIOFUEL(2,1)|CA BEARING SILICATE(2,1)|CA CONTENT(2,1)|CALIBRATION STANDARD(2,1)|CAPTURING CARBON(2,1)|CATION EXCHANGE COLUMN(2,1)|CHARGE BALANCE(2,1)|CHELATOR(2,1)|CHITOSAN(2,1)|CLASSIFICATION(2,1)|CLAWBACK(2,1)|CLIMEWORK(2,1)|COMPACT MASS(2,1)|COMPREHENSIVE PROPOSAL NUMBER(2,1)|COMPUTING V(2,1)|CONFIDENCE(2,1)|CREATED VOID SPACE(2,1)|DCREMAIN(2,1)||(US20240264139)|MINERAL AMENDMENT(100,22)|VERIFICATION(100,17)|REMOVING CARBON(100,12)|ENHANCED ROCK(100,8)|COMMINUTED SILICATE MINERAL(68,3)|SILICATE MINERAL AGGLOMERATION(57,3)|ENHANCED ROCK WEATHERING(46,2)|INTERESTED PARTY(45,1)|RECOVERING SAMPLING COLUMN(38,1)|FUNDAMENTAL ISSUE(37,1)|MINERAL TRANSFORMATION(31,2)|CARBON MEASUREMENT OBJECTIVE(25,1)|LANDOWNER(23,1)|SLOW RELEASE ACIDIFIER(22,3)|IMMOBILE TRACE ELEMENT(21,25)|COMMERCIAL ENTERPRISE(17,1)|GIBBSITE(15,2)|BINDER(14,3)|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)|NEODYMIUM(12,11)|BRUKER PROPRIETARY GEO CALIBRATION(12,1)|VANADIUM(12,1)|EUROPIUM(11,10)|DYSPROSIUM(11,9)|LANTHANUM(11,9)|SAMARIUM(11,8)|SCANDIUM(11,8)|YTTERBIUM(11,8)|GADOLINIUM(11,7)|PRASEODYMIUM(11,6)|BERYLLIUM(11,2)|GERMANIUM(11,2)|RUBIDIUM(11,2)|ZIRCONIUM(11,2)|HOLMIUM(10,6)|LUTETIUM(10,6)|THULIUM(10,6)|DRAWDOWN CALCULATION(10,4)|VROCK MONTE CARLO SIMULATION(10,1)|AVERAGE PARTICLE SIZE(9,4)|ERW(9,4)|BLAST FURNACE SLAG(9,2)|CASO(9,2)|CESIUM(9,2)|CHROMIUM(9,2)|GALLIUM(9,2)|HAFNIUM(9,2)|NIOBIUM(9,2)|RIGOROUS QUANTIFICATION(9,2)|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)|TANTALUM(9,2)|BIOLOGICAL DERIVED COMPONENT(9,1)|PELLETIZED MINERAL AMENDMENT(9,1)|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)|CERIUM(8,9)|YTTRIUM(8,8)|RARE METAL(8,4)|GYPSUM(8,3)|MINERAL SOIL AMENDMENT(8,3)|AIRTIGHT CONTAINMENT(8,2)|NONLIMITING CANDIDATE(8,2)|DELIVER PROSPECTIVE REWARD(8,1)|STERILIZED SOIL BEAKER(8,1)|TRANSITION METAL(7,5)|PPB DETECTION(7,4)|INSTRUMENTAL ERROR(7,3)|COMPUTING VROCK(7,2)|DISSOLUTION KINETICS(7,2)|PHOSPHATE FERTILIZER(7,2)|PULVERIZED SILICATE(7,2)|ALKALIZER KINETICS(7,1)|MINERAL ADDITIVE PROVEN IDENTITY(7,1)|SOIL ORGANIC CARBON(7,1)|TAXONOMY DISTINGUISHE(7,1)|UNINHABITABLE WATERWAY(7,1)|WET BIOMASS WET ALIQUOT(7,1)|CARBON FLUX(6,3)|CHARGE IMBALANCE(6,2)|INORGANIC ADDITIVE(6,2)|MG PPM DETECTION(6,2)|NEUTRAL GROUND(6,2)|ROCK PARTICLE(6,2)|VROCK DOT PRODUCT(6,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)|AGGREGATED PELLET(6,1)|AGLIME SUBSTITUTE(6,1)|AGRICULTURAL SOILS(6,1)|AGRONOMIC PERFORMANCE EXPECTATION(6,1)|ALKALINITY EXPORT(6,1)|BIODEGRADABLE TRANSPORTER(6,1)|BIOFILM MEDIATING(6,1)|CO2 REAGENT AVAILABILITY(6,1)|CO2 UPTAKE(6,1)|CUMULATIVE CATION FLUX MEASURE(6,1)|DDIC DTA ESTIMATE(6,1)|FORSTERITE METRIC TON(6,1)|FORSTERITE TENDENCY(6,1)|HENRY LAW COEFFICIENT(6,1)|INFERRED ION FLUX(6,1)|INSTRUMENTAL UNCERTAINTY(6,1)|INTENSE SCRUTINY(6,1)|MARKETING COLLATERAL(6,1)|MICRONUTRIENT INCORPORATION(6,1)|MYCORRHIZAL INOCULUM(6,1)|NONPROFIT ORGANIZATION(6,1)|OCEAN ACIDIFICATION(6,1)|PELLET AGGLOMERATION(6,1)|PHOSPHORUS ECOSYSTEM LOSS(6,1)|PORTABLE XRF INSTRUMENT(6,1)|PREAPPLICATION SOIL(6,1)|PROTONATED MICROBE(6,1)|PULVERIZED LIMESTONE(6,1)|PULVERIZED MG2SIO(6,1)|RENOWNED CHEMIST(6,1)|RESPIRATORY HEALTH IMPACT(6,1)|REWET BIOMASS(6,1)|RIGOROUS COMPLIANCE(6,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)|SOIL CULTIVATED ZONE(6,1)|SOIL GEOCHEMISTRY(6,1)|SOIL HYDROLOGY(6,1)|NACL SOLUTION(5,4)|PROMETHIUM(5,4)|PULVERIZATION(5,4)|TRIPLICATE(5,4)|CENTRIFUGE CELL(5,3)|BICARBONATE HCO3(5,2)|GROWING PLANT(5,2)|AEROSOL SIZED PARTICLE(5,1)|AGGREGATING GROUND MINERAL(5,1)|ANALYTICAL LABORATORY(5,1)|ANCIENT ROCK FORMATION(5,1)|ANION CONSERVATION(5,1)|CATEGORY REGULATION(5,1)|CATION CONSERVATION(5,1)|CLAUSE XII(5,1)|DIFFERENCE VROCK VECTOR(5,1)|DIFFERENCE VSOIL VECTOR(5,1)|DISSOLVE ALGINATE(5,1)|DISSOLVED ALGINATE POWDER(5,1)|DOWNSTREAM ECOSYSTEM(5,1)|DOWNSTREAM WATERWAY(5,1)|DTA DH INVERSE(5,1)|DUST PREVALENCE(5,1)|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)|FUNGAL ADJUVANT(5,1)|GROUND MINERAL AGGREGATION(5,1)|KEY INSIGHT(5,1)|MICROBIAL CATION EXCHANGER(5,1)|MINERAL ADJUVANT(5,1)|MINERAL TON HECTARE(5,1)|NUTRIENT AVAILABILITY(5,1)|PELLET DISSOLUTION(5,1)|PHOSPHATE ZINC PRECIPITATE(5,1)|PROGRESS FRACTIONATION(5,1)|QUASI GOVERNMENTAL REGULATOR(5,1)|RESERVOIR GEOLOGY(5,1)|SOIL STERILIZATION(5,1)|SPECIALIZED TOOL(5,1)|STEAM STERILIZATION(5,1)|TECHNO ECONOMIC MODELING(5,1)|ULTIMATE PRICE(5,1)|UREY REACTION BASIC PREMISE(5,1)|VERIFICATION VERSION(5,1)|VERIFIED ENHANCED ROCK(5,1)|VOLUNTARY MARKET(5,1)|RARE EARTH ELEMENT(4,18)|AQUEOUS CO2(4,2)|AVOIDED EMISSION(4,2)|CARBONATE SPECIES(4,2)|DISSOLVED CARBONATE(4,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)|MARKET ABILITY(4,2)|MINERAL POTENTIAL(4,2)|SECURE VESSEL(4,2)|SOIL ENVIRONMENT(4,2)|ABUNDANT CO2(4,1)|ACCELERATE TIMING(4,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)|AQUEOUS BICARBONATE MEASUREMENT(4,1)|AQUEOUS COMPLEXATION(4,1)|ASBESTOS EXPOSURE(4,1)|ASSEMBLING MP(4,1)|ATTENDANT DEMAND(4,1)|AUXILIARY GEOCHEMICAL DATA(4,1)|BICARBONATE MOLE(4,1)|BROAD FRAMEWORK(4,1)|CARBON EXCHANGE TRANSACTION(4,1)|CARBON VERIFICATION BENEFIT(4,1)|COARSE PARTICLE(4,1)|COLLECT CELL PELLET(4,1)|CONTINENTAL COLLISION RELEASE(4,1)|CROP HEALTH(4,1)|DISSOLUTION ENHANCING(4,1)|DIVALENT MG(4,1)|EQUILIBRIUM EQUATION(4,1)|FERTILIZATION FREQUENCY(4,1)|FRAUDULENT SAMPLE(4,1)|GROUND NATURAL ENVIRONMENT(4,1)|H2CO SUM(4,1)|INCREASE ECOSYSTEM COBENEFIT(4,1)|LB BROTH(4,1)|MINERAL TRANSFORMATION EXTENT(4,1)|MINUS PROTON DONOR(4,1)|PHOSPHATE LEACHING(4,1)|PHOSPHATE MOBILITY(4,1)|PRECISE ANSWER(4,1)|PREEQUILIBRATED TUBE(4,1)|REACTION THERMODYNAMICS(4,1)|SILICATE MINERAL SHELL(4,1)|SILICATE ROLE(4,1)|UNSEALING SAMPLE(4,1)|VERIFIABLE CARBON REMOVAL(4,1)|XRF ANALYSIS(4,1)|BAG(3,2)|CO2 REMOVAL(3,2)|COMMINUTION(3,2)|FARMER(3,2)|PELLETIZING(3,2)|PRODUCT FORMULATION(3,2)|STAKEHOLDER(3,2)|TOTAL FORMULATION(3,2)|ACIDIC ENVIRONMENT(3,1)|ANALYTICAL PERFORMANCE(3,1)|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)|CARBON MARKET MATURATION(3,1)|CARBON REMOVAL VERIFICATION(3,1)|CARBON TRANSACTION(3,1)|COMPUTING INDEX(3,1)|CORTEVA CARBON(3,1)|DRIED PELLET(3,1)|EMPLACEMENT LOCATION(3,1)|ENTIRE US ECONOMY(3,1)|EXCHANGE COEFFICIENT(3,1)|EXCHANGING RESIN(3,1)|EXPERIMENTAL WORK(3,1)|EXTANT FARM EQUIPMENT(3,1)|FILTRATE ANALYSIS(3,1)|FULL SUMMATION(3,1)|GRIND CELL(3,1)|HEAVY PHOSPHATE(3,1)|ICP ANALYSIS(3,1)|IMMOBILIZATION(3,1)|INDIGO CARBON(3,1)|LABORATORY SETTING(3,1)|MARINE SETTING(3,1)|MG MINERAL(3,1)|MINERAL DELIVERY(3,1)|MINERAL DISSOLUTION RATE(3,1)|NATURAL ABUNDANCE CALCULATION(3,1)|NATURAL SOILS(3,1)|NEGATIVE EMISSION(3,1)|PLANT DEMAND(3,1)|PROJECT EVALUATION CRITERIA(3,1)|RELEVANT ION(3,1)|ROCK ELEMENTAL ANALYSIS(3,1)|ROCK MATERIAL ACCELERATED WEATHERING(3,1)|SAMPLING DENSITY(3,1)|SHARP THRESHOLD(3,1)|SOIL ELEMENTAL ANALYSIS(3,1)|SUBSURFACE SOIL PORE WATER(3,1)|TECHNOLOGICAL SOLUTION(3,1)|WET GRAM(3,1)|ANALYTICAL CHEMISTRY(2,3)|LYSE(2,3)|SOIL SAMPLE(2,3)|ABILITY THRESHOLD(2,1)|ACCEPTANCE(2,1)|ACCOUNTING(2,1)|ACID TREATED ARTHROBACTER(2,1)|ACIDIC SOIL SOLUTION(2,1)|ADDITIONALITY(2,1)|ADMIXTURE(2,1)|AERATION(2,1)|AGLIME MESH SIZE OBSERVATION(2,1)|AGRICULTURE(2,1)|ALGAL BLOOM(2,1)|ANALYTICAL SOLUTION(2,1)|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)|ATTRACTION(2,1)|AUTOCLAVE(2,1)|BACTERIA(2,1)|BIOADSORBED METAL ACTIVE RELEASE(2,1)|BIOFUEL(2,1)|CA BEARING SILICATE(2,1)|CA CONTENT(2,1)|CALIBRATION STANDARD(2,1)|CAPTURING CARBON(2,1)|CATION EXCHANGE COLUMN(2,1)|CHARGE BALANCE(2,1)|CHELATOR(2,1)|CHITOSAN(2,1)|CLASSIFICATION(2,1)|CLAWBACK(2,1)|CLIMEWORK(2,1)|CO2 MOLECULAR MASS(2,1)|COMPACT MASS(2,1)|COMPREHENSIVE PROPOSAL NUMBER(2,1)||(US11921098)|MINERAL AMENDMENT(100,22)|VERIFICATION(100,18)|REMOVING CARBON(100,13)|ENHANCED ROCK(100,9)|SILICATE MINERAL AGGLOMERATION(66,2)|COMMINUTED SILICATE MINERAL(57,3)|ENHANCED ROCK WEATHERING(46,2)|INTERESTED PARTY(45,1)|RECOVERING SAMPLING COLUMN(38,1)|FUNDAMENTAL ISSUE(37,1)|MINERAL TRANSFORMATION(31,2)|CARBON MEASUREMENT OBJECTIVE(25,1)|LANDOWNER(23,1)|SLOW RELEASE ACIDIFIER(22,3)|IMMOBILE TRACE ELEMENT(21,25)|COMMERCIAL ENTERPRISE(17,1)|GIBBSITE(15,2)|BINDER(14,3)|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)|NEODYMIUM(12,11)|BRUKER PROPRIETARY GEO CALIBRATION(12,1)|VANADIUM(12,1)|EUROPIUM(11,10)|DYSPROSIUM(11,9)|LANTHANUM(11,9)|SAMARIUM(11,8)|SCANDIUM(11,8)|YTTERBIUM(11,8)|GADOLINIUM(11,7)|PRASEODYMIUM(11,6)|BERYLLIUM(11,2)|GERMANIUM(11,2)|RUBIDIUM(11,2)|ZIRCONIUM(11,2)|HOLMIUM(10,6)|LUTETIUM(10,6)|THULIUM(10,6)|DRAWDOWN CALCULATION(10,4)|VROCK MONTE CARLO SIMULATION(10,1)|AVERAGE PARTICLE SIZE(9,4)|ERW(9,4)|BLAST FURNACE SLAG(9,2)|CASO(9,2)|CESIUM(9,2)|CHROMIUM(9,2)|GALLIUM(9,2)|HAFNIUM(9,2)|NIOBIUM(9,2)|RIGOROUS QUANTIFICATION(9,2)|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)|TANTALUM(9,2)|BIOLOGICAL DERIVED COMPONENT(9,1)|PELLETIZED MINERAL AMENDMENT(9,1)|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)|CERIUM(8,9)|YTTRIUM(8,8)|RARE METAL(8,4)|GYPSUM(8,3)|MINERAL SOIL AMENDMENT(8,3)|AIRTIGHT CONTAINMENT(8,2)|NONLIMITING CANDIDATE(8,2)|DELIVER PROSPECTIVE REWARD(8,1)|STERILIZED SOIL BEAKER(8,1)|TRANSITION METAL(7,5)|PPB DETECTION(7,4)|INSTRUMENTAL ERROR(7,3)|COMPUTING VROCK(7,2)|DISSOLUTION KINETICS(7,2)|PHOSPHATE FERTILIZER(7,2)|PULVERIZED SILICATE(7,2)|ALKALIZER KINETICS(7,1)|MINERAL ADDITIVE PROVEN IDENTITY(7,1)|SOIL ORGANIC CARBON(7,1)|TAXONOMY DISTINGUISHE(7,1)|UNINHABITABLE WATERWAY(7,1)|WET BIOMASS WET ALIQUOT(7,1)|CARBON FLUX(6,3)|CHARGE IMBALANCE(6,2)|INORGANIC ADDITIVE(6,2)|MG PPM DETECTION(6,2)|NEUTRAL GROUND(6,2)|ROCK PARTICLE(6,2)|VROCK DOT PRODUCT(6,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)|AGGREGATED PELLET(6,1)|AGLIME SUBSTITUTE(6,1)|AGRICULTURAL SOILS(6,1)|AGRONOMIC PERFORMANCE EXPECTATION(6,1)|ALKALINITY EXPORT(6,1)|BIODEGRADABLE TRANSPORTER(6,1)|BIOFILM MEDIATING(6,1)|CO2 REAGENT AVAILABILITY(6,1)|CO2 UPTAKE(6,1)|CUMULATIVE CATION FLUX MEASURE(6,1)|DDIC DTA ESTIMATE(6,1)|FORSTERITE METRIC TON(6,1)|FORSTERITE TENDENCY(6,1)|HENRY LAW COEFFICIENT(6,1)|INFERRED ION FLUX(6,1)|INSTRUMENTAL UNCERTAINTY(6,1)|INTENSE SCRUTINY(6,1)|MARKETING COLLATERAL(6,1)|MICRONUTRIENT INCORPORATION(6,1)|MYCORRHIZAL INOCULUM(6,1)|NONPROFIT ORGANIZATION(6,1)|OCEAN ACIDIFICATION(6,1)|PELLET AGGLOMERATION(6,1)|PHOSPHORUS ECOSYSTEM LOSS(6,1)|PORTABLE XRF INSTRUMENT(6,1)|PREAPPLICATION SOIL(6,1)|PROTONATED MICROBE(6,1)|PULVERIZED LIMESTONE(6,1)|PULVERIZED MG2SIO(6,1)|RENOWNED CHEMIST(6,1)|RESPIRATORY HEALTH IMPACT(6,1)|REWET BIOMASS(6,1)|RIGOROUS COMPLIANCE(6,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)|SOIL CULTIVATED ZONE(6,1)|SOIL GEOCHEMISTRY(6,1)|SOIL HYDROLOGY(6,1)|NACL SOLUTION(5,4)|PROMETHIUM(5,4)|PULVERIZATION(5,4)|TRIPLICATE(5,4)|CENTRIFUGE CELL(5,3)|BICARBONATE HCO3(5,2)|AEROSOL SIZED PARTICLE(5,1)|AGGREGATING GROUND MINERAL(5,1)|ANALYTICAL LABORATORY(5,1)|ANCIENT ROCK FORMATION(5,1)|ANION CONSERVATION(5,1)|CATEGORY REGULATION(5,1)|CATION CONSERVATION(5,1)|CLAUSE XII(5,1)|DIFFERENCE VROCK VECTOR(5,1)|DIFFERENCE VSOIL VECTOR(5,1)|DISSOLVE ALGINATE(5,1)|DISSOLVED ALGINATE POWDER(5,1)|DOWNSTREAM ECOSYSTEM(5,1)|DOWNSTREAM WATERWAY(5,1)|DTA DH INVERSE(5,1)|DUST PREVALENCE(5,1)|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)|FUNGAL ADJUVANT(5,1)|GROUND MINERAL AGGREGATION(5,1)|KEY INSIGHT(5,1)|MICROBIAL CATION EXCHANGER(5,1)|MINERAL ADJUVANT(5,1)|MINERAL TON HECTARE(5,1)|NUTRIENT AVAILABILITY(5,1)|PELLET DISSOLUTION(5,1)|PHOSPHATE ZINC PRECIPITATE(5,1)|PROGRESS FRACTIONATION(5,1)|QUASI GOVERNMENTAL REGULATOR(5,1)|RESERVOIR GEOLOGY(5,1)|SOIL STERILIZATION(5,1)|SPECIALIZED TOOL(5,1)|STEAM STERILIZATION(5,1)|TECHNO ECONOMIC MODELING(5,1)|ULTIMATE PRICE(5,1)|UREY REACTION BASIC PREMISE(5,1)|VERIFICATION VERSION(5,1)|VERIFIED ENHANCED ROCK(5,1)|VOLUNTARY MARKET(5,1)|RARE EARTH ELEMENT(4,18)|AQUEOUS CO2(4,2)|AVOIDED EMISSION(4,2)|CARBONATE SPECIES(4,2)|DISSOLVED CARBONATE(4,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)|MARKET ABILITY(4,2)|MINERAL POTENTIAL(4,2)|SECURE VESSEL(4,2)|SOIL ENVIRONMENT(4,2)|ABUNDANT CO2(4,1)|ACCELERATE TIMING(4,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)|AQUEOUS BICARBONATE MEASUREMENT(4,1)|AQUEOUS COMPLEXATION(4,1)|ASBESTOS EXPOSURE(4,1)|ASSEMBLING MP(4,1)|ATTENDANT DEMAND(4,1)|AUXILIARY GEOCHEMICAL DATA(4,1)|BICARBONATE MOLE(4,1)|BROAD FRAMEWORK(4,1)|CARBON EXCHANGE TRANSACTION(4,1)|CARBON VERIFICATION BENEFIT(4,1)|COARSE PARTICLE(4,1)|COLLECT CELL PELLET(4,1)|CONTINENTAL COLLISION RELEASE(4,1)|CROP HEALTH(4,1)|DISSOLUTION ENHANCING(4,1)|DIVALENT MG(4,1)|EQUILIBRIUM EQUATION(4,1)|FERTILIZATION FREQUENCY(4,1)|FRAUDULENT SAMPLE(4,1)|GROUND NATURAL ENVIRONMENT(4,1)|H2CO SUM(4,1)|INCREASE ECOSYSTEM COBENEFIT(4,1)|LB BROTH(4,1)|MINERAL TRANSFORMATION EXTENT(4,1)|MINUS PROTON DONOR(4,1)|PHOSPHATE LEACHING(4,1)|PHOSPHATE MOBILITY(4,1)|PRECISE ANSWER(4,1)|PREEQUILIBRATED TUBE(4,1)|REACTION THERMODYNAMICS(4,1)|SECURITIZED CARBON REMOVAL(4,1)|SILICATE MINERAL SHELL(4,1)|SILICATE ROLE(4,1)|UNSEALING SAMPLE(4,1)|VERIFIABLE CARBON REMOVAL(4,1)|XRF ANALYSIS(4,1)|BAG(3,2)|CO2 REMOVAL(3,2)|COMMINUTION(3,2)|FARMER(3,2)|PELLETIZING(3,2)|PRODUCT FORMULATION(3,2)|STAKEHOLDER(3,2)|TOTAL FORMULATION(3,2)|ACIDIC ENVIRONMENT(3,1)|ANALYTICAL PERFORMANCE(3,1)|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)|CARBON MARKET MATURATION(3,1)|CARBON REMOVAL VERIFICATION(3,1)|CARBON TRANSACTION(3,1)|COMPUTING INDEX(3,1)|CORTEVA CARBON(3,1)|DRIED PELLET(3,1)|EMPLACEMENT LOCATION(3,1)|ENTIRE US ECONOMY(3,1)|EXCHANGE COEFFICIENT(3,1)|EXCHANGING RESIN(3,1)|EXPERIMENTAL WORK(3,1)|EXTANT FARM EQUIPMENT(3,1)|FILTRATE ANALYSIS(3,1)|FULL SUMMATION(3,1)|GRIND CELL(3,1)|GROWING PLANT(3,1)|HEAVY PHOSPHATE(3,1)|ICP ANALYSIS(3,1)|IMMOBILIZATION(3,1)|INDIGO CARBON(3,1)|LABORATORY SETTING(3,1)|MARINE SETTING(3,1)|MINERAL DELIVERY(3,1)|MINERAL DISSOLUTION RATE(3,1)|NATURAL ABUNDANCE CALCULATION(3,1)|NATURAL SOILS(3,1)|NEGATIVE EMISSION(3,1)|PROJECT EVALUATION CRITERIA(3,1)|RELEVANT ION(3,1)|ROCK ELEMENTAL ANALYSIS(3,1)|ROCK MATERIAL ACCELERATED WEATHERING(3,1)|SAMPLING DENSITY(3,1)|SHARP THRESHOLD(3,1)|SOIL ELEMENTAL ANALYSIS(3,1)|SUBSURFACE SOIL PORE WATER(3,1)|TECHNOLOGICAL SOLUTION(3,1)|WET GRAM(3,1)|ANALYTICAL CHEMISTRY(2,3)|LYSE(2,3)|SOIL SAMPLE(2,3)|ABILITY THRESHOLD(2,1)|ACCEPTANCE(2,1)|ACCOUNTING(2,1)|ACID TREATED ARTHROBACTER(2,1)|ACIDIC SOIL SOLUTION(2,1)|ADDITIONALITY(2,1)|ADMIXTURE(2,1)|AERATION(2,1)|AGLIME MESH SIZE OBSERVATION(2,1)|AGRICULTURE(2,1)|ALGAL BLOOM(2,1)|ANALYTICAL SOLUTION(2,1)|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)|ATTRACTION(2,1)|AUTOCLAVE(2,1)|BACTERIA(2,1)|BIOADSORBED METAL ACTIVE RELEASE(2,1)|BIOFUEL(2,1)|CA BEARING SILICATE(2,1)|CA CONTENT(2,1)|CALIBRATION STANDARD(2,1)|CAPTURING CARBON(2,1)|CATION EXCHANGE COLUMN(2,1)|CHARGE BALANCE(2,1)|CHELATOR(2,1)|CHITOSAN(2,1)|CLASSIFICATION(2,1)|CLAWBACK(2,1)|CLIMEWORK(2,1)|CO2 MOLECULAR MASS(2,1)|COMPACT MASS(2,1)|COMPREHENSIVE PROPOSAL NUMBER(2,1)||(US20230273174)|MINERAL AMENDMENT(100,22)|VERIFICATION(100,18)|REMOVING CARBON(100,13)|ENHANCED ROCK(100,8)|SILICATE MINERAL AGGLOMERATION(66,2)|COMMINUTED SILICATE MINERAL(57,3)|ENHANCED ROCK WEATHERING(46,2)|INTERESTED PARTY(45,1)|FUNDAMENTAL ISSUE(37,1)|MINERAL TRANSFORMATION(31,2)|SAMPLING COLUMN(27,1)|CARBON MEASUREMENT OBJECTIVE(25,1)|LANDOWNER(23,1)|SLOW RELEASE ACIDIFIER(22,3)|IMMOBILE TRACE ELEMENT(21,25)|COMMERCIAL ENTERPRISE(17,1)|GIBBSITE(15,2)|BINDER(14,3)|NEODYMIUM(12,11)|BRUKER PROPRIETARY GEO CALIBRATION(12,1)|VANADIUM(12,1)|EUROPIUM(11,10)|DYSPROSIUM(11,9)|LANTHANUM(11,9)|SAMARIUM(11,8)|SCANDIUM(11,8)|YTTERBIUM(11,8)|GADOLINIUM(11,7)|PRASEODYMIUM(11,6)|BERYLLIUM(11,2)|GERMANIUM(11,2)|RUBIDIUM(11,2)|ZIRCONIUM(11,2)|HOLMIUM(10,6)|LUTETIUM(10,6)|THULIUM(10,6)|DRAWDOWN CALCULATION(10,4)|VROCK MONTE CARLO SIMULATION(10,1)|AVERAGE PARTICLE SIZE(9,4)|ERW(9,4)|BLAST FURNACE SLAG(9,2)|CASO(9,2)|CESIUM(9,2)|CHROMIUM(9,2)|GALLIUM(9,2)|HAFNIUM(9,2)|NIOBIUM(9,2)|RIGOROUS QUANTIFICATION(9,2)|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)|TANTALUM(9,2)|BIOLOGICAL DERIVED COMPONENT(9,1)|DIVERSE DECARBONIZATION STRATEGY(9,1)|PELLETIZED MINERAL AMENDMENT(9,1)|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)|CERIUM(8,9)|YTTRIUM(8,8)|RARE METAL(8,4)|GYPSUM(8,3)|MINERAL SOIL AMENDMENT(8,3)|AIRTIGHT CONTAINMENT(8,2)|NONLIMITING CANDIDATE(8,2)|DELIVER PROSPECTIVE REWARD(8,1)|STERILIZED SOIL BEAKER(8,1)|TRANSITION METAL(7,5)|PPB DETECTION(7,4)|INSTRUMENTAL ERROR(7,3)|COMPUTING VROCK(7,2)|DISSOLUTION KINETICS(7,2)|PHOSPHATE FERTILIZER(7,2)|PULVERIZED SILICATE(7,2)|ALKALIZER KINETICS(7,1)|MINERAL ADDITIVE PROVEN IDENTITY(7,1)|SOIL ORGANIC CARBON(7,1)|TAXONOMY DISTINGUISHE(7,1)|UNINHABITABLE WATERWAY(7,1)|WET BIOMASS WET ALIQUOT(7,1)|CARBON FLUX(6,3)|CHARGE IMBALANCE(6,2)|INORGANIC ADDITIVE(6,2)|MG PPM DETECTION(6,2)|NEUTRAL GROUND(6,2)|ROCK PARTICLE(6,2)|VROCK DOT PRODUCT(6,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)|AGGREGATED PELLET(6,1)|AGLIME SUBSTITUTE(6,1)|AGRICULTURAL SOILS(6,1)|AGRONOMIC PERFORMANCE EXPECTATION(6,1)|ALKALINITY EXPORT(6,1)|BIODEGRADABLE TRANSPORTER(6,1)|BIOFILM MEDIATING(6,1)|CO2 REAGENT AVAILABILITY(6,1)|CO2 UPTAKE(6,1)|CUMULATIVE CATION FLUX MEASURE(6,1)|DDIC DTA ESTIMATE(6,1)|FORSTERITE METRIC TON(6,1)|FORSTERITE TENDENCY(6,1)|HENRY LAW COEFFICIENT(6,1)|INFERRED ION FLUX(6,1)|INSTRUMENTAL UNCERTAINTY(6,1)|INTENSE SCRUTINY(6,1)|MARKETING COLLATERAL(6,1)|MICRONUTRIENT INCORPORATION(6,1)|MYCORRHIZAL INOCULUM(6,1)|NONPROFIT ORGANIZATION(6,1)|OCEAN ACIDIFICATION(6,1)|PELLET AGGLOMERATION(6,1)|PHOSPHORUS ECOSYSTEM LOSS(6,1)|PORTABLE XRF INSTRUMENT(6,1)|PREAPPLICATION SOIL(6,1)|PROTONATED MICROBE(6,1)|PULVERIZED LIMESTONE(6,1)|PULVERIZED MG2SIO(6,1)|RENOWNED CHEMIST(6,1)|RESPIRATORY HEALTH IMPACT(6,1)|REWET BIOMASS(6,1)|RIGOROUS COMPLIANCE(6,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)|SOIL CULTIVATED ZONE(6,1)|SOIL GEOCHEMISTRY(6,1)|SOIL HYDROLOGY(6,1)|NACL SOLUTION(5,4)|PROMETHIUM(5,4)|PULVERIZATION(5,4)|TRIPLICATE(5,4)|CENTRIFUGE CELL(5,3)|BICARBONATE HCO3(5,2)|GROWING PLANT(5,2)|AEROSOL SIZED PARTICLE(5,1)|AGGREGATING GROUND MINERAL(5,1)|ANALYTICAL LABORATORY(5,1)|ANCIENT ROCK FORMATION(5,1)|ANION CONSERVATION(5,1)|CATEGORY REGULATION(5,1)|CATION CONSERVATION(5,1)|CLAUSE XII(5,1)|DIFFERENCE VROCK VECTOR(5,1)|DIFFERENCE VSOIL VECTOR(5,1)|DISSOLVE ALGINATE(5,1)|DISSOLVED ALGINATE POWDER(5,1)|DOWNSTREAM ECOSYSTEM(5,1)|DOWNSTREAM WATERWAY(5,1)|DTA DH INVERSE(5,1)|DUST PREVALENCE(5,1)|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)|FUNGAL ADJUVANT(5,1)|GROUND MINERAL AGGREGATION(5,1)|KEY INSIGHT(5,1)|MICROBIAL CATION EXCHANGER(5,1)|MINERAL ADJUVANT(5,1)|NUTRIENT AVAILABILITY(5,1)|PELLET DISSOLUTION(5,1)|PHOSPHATE ZINC PRECIPITATE(5,1)|PROGRESS FRACTIONATION(5,1)|QUASI GOVERNMENTAL REGULATOR(5,1)|RESERVOIR GEOLOGY(5,1)|SOIL STERILIZATION(5,1)|SPECIALIZED TOOL(5,1)|STEAM STERILIZATION(5,1)|TECHNO ECONOMIC MODELING(5,1)|ULTIMATE PRICE(5,1)|VERIFICATION VERSION(5,1)|VERIFIED ENHANCED ROCK(5,1)|VOLUNTARY MARKET(5,1)|RARE EARTH ELEMENT(4,18)|AQUEOUS CO2(4,2)|AVOIDED EMISSION(4,2)|CARBONATE SPECIES(4,2)|DISSOLVED CARBONATE(4,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)|MARKET ABILITY(4,2)|MINERAL POTENTIAL(4,2)|SECURE VESSEL(4,2)|SOIL ENVIRONMENT(4,2)|ABUNDANT CO2(4,1)|ACCELERATE TIMING(4,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)|AQUEOUS BICARBONATE MEASUREMENT(4,1)|AQUEOUS COMPLEXATION(4,1)|ASBESTOS EXPOSURE(4,1)|ASSEMBLING MP(4,1)|ATTENDANT DEMAND(4,1)|AUXILIARY GEOCHEMICAL DATA(4,1)|BICARBONATE MOLE(4,1)|BROAD FRAMEWORK(4,1)|CARBON EXCHANGE TRANSACTION(4,1)|CARBON VERIFICATION BENEFIT(4,1)|COARSE PARTICLE(4,1)|COLLECT CELL PELLET(4,1)|CONTINENTAL COLLISION RELEASE(4,1)|CROP HEALTH(4,1)|DISSOLUTION ENHANCING(4,1)|DIVALENT MG(4,1)|EQUILIBRIUM EQUATION(4,1)|FERTILIZATION FREQUENCY(4,1)|FRAUDULENT SAMPLE(4,1)|GROUND NATURAL ENVIRONMENT(4,1)|H2CO SUM(4,1)|INCREASE ECOSYSTEM COBENEFIT(4,1)|LB BROTH(4,1)|MINERAL TRANSFORMATION EXTENT(4,1)|MINUS PROTON DONOR(4,1)|PHOSPHATE LEACHING(4,1)|PHOSPHATE MOBILITY(4,1)|PRECISE ANSWER(4,1)|PREEQUILIBRATED TUBE(4,1)|REACTION THERMODYNAMICS(4,1)|SECURITIZED CARBON REMOVAL(4,1)|SILICATE MINERAL SHELL(4,1)|SILICATE ROLE(4,1)|UNSEALING SAMPLE(4,1)|VERIFIABLE CARBON REMOVAL(4,1)|XRF ANALYSIS(4,1)|BAG(3,2)|CO2 REMOVAL(3,2)|COMMINUTION(3,2)|FARMER(3,2)|PELLETIZING(3,2)|PRODUCT FORMULATION(3,2)|STAKEHOLDER(3,2)|TOTAL FORMULATION(3,2)|ACIDIC ENVIRONMENT(3,1)|ANALYTICAL PERFORMANCE(3,1)|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)|CARBON MARKET MATURATION(3,1)|CARBON REMOVAL VERIFICATION(3,1)|CARBON TRANSACTION(3,1)|COMPUTING INDEX(3,1)|CORTEVA CARBON(3,1)|DRIED PELLET(3,1)|EMPLACEMENT LOCATION(3,1)|ENTIRE US ECONOMY(3,1)|EXCHANGE COEFFICIENT(3,1)|EXCHANGING RESIN(3,1)|EXPERIMENTAL WORK(3,1)|EXTANT FARM EQUIPMENT(3,1)|FILTRATE ANALYSIS(3,1)|FULL SUMMATION(3,1)|GRIND CELL(3,1)|HEAVY PHOSPHATE(3,1)|ICP ANALYSIS(3,1)|IMMOBILIZATION(3,1)|INDIGO CARBON(3,1)|LABORATORY SETTING(3,1)|MARINE SETTING(3,1)|MINERAL DELIVERY(3,1)|MINERAL DISSOLUTION RATE(3,1)|NATURAL ABUNDANCE CALCULATION(3,1)|NATURAL SOILS(3,1)|NEGATIVE EMISSION(3,1)|PLANT DEMAND(3,1)|PROJECT EVALUATION CRITERIA(3,1)|RELEVANT ION(3,1)|ROCK ELEMENTAL ANALYSIS(3,1)|ROCK MATERIAL ACCELERATED WEATHERING(3,1)|SAMPLING DENSITY(3,1)|SHARP THRESHOLD(3,1)|SOIL ELEMENTAL ANALYSIS(3,1)|SUBSURFACE SOIL PORE WATER(3,1)|TECHNOLOGICAL SOLUTION(3,1)|WET GRAM(3,1)|ANALYTICAL CHEMISTRY(2,3)|LYSE(2,3)|SOIL SAMPLE(2,3)|ABILITY THRESHOLD(2,1)|ACCEPTANCE(2,1)|ACCOUNTING(2,1)|ACID TREATED ARTHROBACTER(2,1)|ACIDIC SOIL SOLUTION(2,1)|ADDITIONALITY(2,1)|ADMIXTURE(2,1)|AERATION(2,1)|AGLIME MESH SIZE OBSERVATION(2,1)|AGRICULTURE(2,1)|ALGAL BLOOM(2,1)|ANALYTICAL SOLUTION(2,1)|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)|ATTRACTION(2,1)|AUTOCLAVE(2,1)|BACTERIA(2,1)|BIOADSORBED METAL ACTIVE RELEASE(2,1)|BIOFUEL(2,1)|CA BEARING SILICATE(2,1)|CA CONTENT(2,1)|CALIBRATION STANDARD(2,1)|CAPTURING CARBON(2,1)|CATION EXCHANGE COLUMN(2,1)|CHARGE BALANCE(2,1)|CHELATOR(2,1)|CHITOSAN(2,1)|CLASSIFICATION(2,1)|CLAWBACK(2,1)|CLIMEWORK(2,1)|CO2 MOLECULAR MASS(2,1)|COMPACT MASS(2,1)||(US11644454)|MINERAL AMENDMENT(100,20)|VERIFICATION(100,18)|REMOVING CARBON(100,12)|ENHANCED ROCK(100,8)|ENHANCED ROCK WEATHERING(100,3)|INTERESTED PARTY(42,1)|FUNDAMENTAL ISSUE(35,1)|IMMOBILE TRACE ELEMENT(33,30)|SAMPLING COLUMN(26,1)|CARBON MEASUREMENT OBJECTIVE(24,1)|IMMOBILE TRACE ELEMENT ABUNDANCE(22,1)|LANDOWNER(22,1)|SOIL SAMPLE(21,10)|DIVALENT CATION MEASUREMENT(20,2)|COMMERCIAL ENTERPRISE(16,1)|MINERAL AMENDMENT ADDITION(12,1)|VANADIUM(12,1)|NEODYMIUM(11,11)|EUROPIUM(11,10)|DYSPROSIUM(11,9)|PRASEODYMIUM(11,6)|BRUKER PROPRIETARY GEO CALIBRATION(11,1)|LANTHANUM(10,9)|SAMARIUM(10,8)|SCANDIUM(10,8)|YTTERBIUM(10,8)|GADOLINIUM(10,7)|HOLMIUM(10,6)|LUTETIUM(10,6)|THULIUM(10,6)|BERYLLIUM(10,2)|GERMANIUM(10,2)|RUBIDIUM(10,2)|ZIRCONIUM(10,2)|DRAWDOWN CALCULATION(9,4)|ERW(9,4)|GALLIUM(9,2)|HAFNIUM(9,2)|NIOBIUM(9,2)|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)|TANTALUM(9,2)|VROCK MONTE CARLO SIMULATION(9,1)|CERIUM(8,9)|YTTRIUM(8,8)|RARE METAL(8,4)|MINERAL SOIL AMENDMENT(8,3)|AIRTIGHT CONTAINMENT(8,2)|CESIUM(8,2)|CHROMIUM(8,2)|NONLIMITING CANDIDATE(8,2)|RIGOROUS QUANTIFICATION(8,2)|DELIVER PROSPECTIVE REWARD(8,1)|DIVERSE DECARBONIZATION STRATEGY(8,1)|PELLETIZED MINERAL AMENDMENT(8,1)|SCIENCE SUPPORTIVE ECOSYSTEM(8,1)|STERILIZED SOIL BEAKER(8,1)|ETHYLENEDIAMINETETRAACETIC ACID(7,4)|PPB DETECTION(7,4)|INSTRUMENTAL ERROR(7,3)|PHOSPHATE FERTILIZER(7,2)|ALKALIZER KINETICS(7,1)|MINERAL ADDITIVE PROVEN IDENTITY(7,1)|SOIL ORGANIC CARBON(7,1)|TAXONOMY DISTINGUISHE(7,1)|UNINHABITABLE WATERWAY(7,1)|WET BIOMASS WET ALIQUOT(7,1)|TRANSITION METAL(6,5)|CARBON FLUX(6,3)|APPLIED DIVALENT CATION(6,2)|COMPUTING VROCK(6,2)|DISSOLUTION KINETICS(6,2)|PULVERIZED SILICATE(6,2)|ROCK PARTICLE(6,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)|ALKALINITY EXPORT(6,1)|BIODEGRADABLE TRANSPORTER(6,1)|CO2 REAGENT AVAILABILITY(6,1)|CUMULATIVE CATION FLUX MEASURE(6,1)|FORSTERITE METRIC TON(6,1)|HENRY LAW COEFFICIENT(6,1)|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(6,1)|INSTRUMENTAL UNCERTAINTY(6,1)|MICRONUTRIENT INCORPORATION(6,1)|MYCORRHIZAL INOCULUM(6,1)|PELLET AGGLOMERATION(6,1)|PORTABLE XRF INSTRUMENT(6,1)|RESPIRATORY HEALTH IMPACT(6,1)|CENTRIFUGE CELL(5,3)|BICARBONATE HCO3(5,2)|CHARGE IMBALANCE(5,2)|GROWING PLANT(5,2)|INORGANIC ADDITIVE(5,2)|MG PPM DETECTION(5,2)|NEUTRAL GROUND(5,2)|VROCK DOT PRODUCT(5,2)|AGGREGATED PELLET(5,1)|AGLIME SUBSTITUTE(5,1)|AGRICULTURAL SOILS(5,1)|AGRONOMIC PERFORMANCE EXPECTATION(5,1)|BIOFILM MEDIATING(5,1)|CO2 UPTAKE(5,1)|DDIC DTA ESTIMATE(5,1)|FORSTERITE TENDENCY(5,1)|INFERRED ION FLUX(5,1)|INTENSE SCRUTINY(5,1)|MARKETING COLLATERAL(5,1)|NONPROFIT ORGANIZATION(5,1)|OCEAN ACIDIFICATION(5,1)|PHOSPHORUS ECOSYSTEM LOSS(5,1)|PREAPPLICATION SOIL(5,1)|PROTONATED MICROBE(5,1)|PULVERIZED LIMESTONE(5,1)|PULVERIZED MG2SIO(5,1)|RENOWNED CHEMIST(5,1)|REWET BIOMASS(5,1)|RIGOROUS COMPLIANCE(5,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(5,1)|SOIL CULTIVATED ZONE(5,1)|SOIL GEOCHEMISTRY(5,1)|SOIL HYDROLOGY(5,1)|X RAY FLUORESCENCE SPECTROSCOPY(5,1)|RARE EARTH ELEMENT(4,18)|NACL SOLUTION(4,4)|PROMETHIUM(4,4)|PULVERIZATION(4,4)|TRIPLICATE(4,4)|AQUEOUS CO2(4,2)|AVOIDED EMISSION(4,2)|CARBONATE SPECIES(4,2)|DISSOLVED CARBONATE(4,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)|MARKET ABILITY(4,2)|MINERAL POTENTIAL(4,2)|SOIL ENVIRONMENT(4,2)|ABUNDANT CO2(4,1)|ACCELERATE TIMING(4,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)|AEROSOL SIZED PARTICLE(4,1)|AGGREGATING GROUND MINERAL(4,1)|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)|ANALYTICAL LABORATORY(4,1)|ANCIENT ROCK FORMATION(4,1)|ANION CONSERVATION(4,1)|AQUEOUS BICARBONATE MEASUREMENT(4,1)|AQUEOUS COMPLEXATION(4,1)|ASBESTOS EXPOSURE(4,1)|ASSEMBLING MP(4,1)|ATTENDANT DEMAND(4,1)|AUXILIARY GEOCHEMICAL DATA(4,1)|BICARBONATE MOLE(4,1)|BROAD FRAMEWORK(4,1)|CARBON EXCHANGE TRANSACTION(4,1)|CARBON VERIFICATION BENEFIT(4,1)|CATEGORY REGULATION(4,1)|CATION CONSERVATION(4,1)|CLAUSE XII(4,1)|COARSE PARTICLE(4,1)|COLLECT CELL PELLET(4,1)|CONTINENTAL COLLISION RELEASE(4,1)|CROP HEALTH(4,1)|DIFFERENCE VROCK VECTOR(4,1)|DIFFERENCE VSOIL VECTOR(4,1)|DISSOLUTION ENHANCING(4,1)|DISSOLVE ALGINATE(4,1)|DISSOLVED ALGINATE POWDER(4,1)|DIVALENT MG(4,1)|DOWNSTREAM ECOSYSTEM(4,1)|DOWNSTREAM WATERWAY(4,1)|DTA DH INVERSE(4,1)|DUST PREVALENCE(4,1)|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)|EQUILIBRIUM EQUATION(4,1)|FERTILIZATION FREQUENCY(4,1)|FRAUDULENT SAMPLE(4,1)|FUNGAL ADJUVANT(4,1)|GROUND MINERAL AGGREGATION(4,1)|GROUND NATURAL ENVIRONMENT(4,1)|H2CO SUM(4,1)|INCREASE ECOSYSTEM COBENEFIT(4,1)|KEY INSIGHT(4,1)|LB BROTH(4,1)|MICROBIAL CATION EXCHANGER(4,1)|MINERAL ADJUVANT(4,1)|MINERAL TRANSFORMATION EXTENT(4,1)|MINUS PROTON DONOR(4,1)|NUTRIENT AVAILABILITY(4,1)|PELLET DISSOLUTION(4,1)|PHOSPHATE LEACHING(4,1)|PHOSPHATE MOBILITY(4,1)|PRECISE ANSWER(4,1)|PREEQUILIBRATED TUBE(4,1)|PROGRESS FRACTIONATION(4,1)|QUASI GOVERNMENTAL REGULATOR(4,1)|REACTION THERMODYNAMICS(4,1)|RESERVOIR GEOLOGY(4,1)|SECURITIZED CARBON REMOVAL(4,1)|SILICATE MINERAL SHELL(4,1)|SILICATE ROLE(4,1)|SOIL STERILIZATION(4,1)|SPECIALIZED TOOL(4,1)|STEAM STERILIZATION(4,1)|TECHNO ECONOMIC MODELING(4,1)|ULTIMATE PRICE(4,1)|UNSEALING SAMPLE(4,1)|UREY REACTION BASIC PREMISE(4,1)|VERIFIABLE CARBON REMOVAL(4,1)|VERIFICATION VERSION(4,1)|VERIFIED ENHANCED ROCK(4,1)|VOLUNTARY MARKET(4,1)|XRF ANALYSIS(4,1)|CARBON DIOXIDE REMOVAL(3,10)|BAG(3,2)|BINDER(3,2)|CO2 REMOVAL(3,2)|COMMINUTION(3,2)|FARMER(3,2)|PELLETIZING(3,2)|PRODUCT FORMULATION(3,2)|STAKEHOLDER(3,2)|TOTAL FORMULATION(3,2)|ACIDIC ENVIRONMENT(3,1)|ANALYTICAL PERFORMANCE(3,1)|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)|CARBON MARKET MATURATION(3,1)|CARBON REMOVAL VERIFICATION(3,1)|CARBON TRANSACTION(3,1)|COMPUTING INDEX(3,1)|CORTEVA CARBON(3,1)|DRIED PELLET(3,1)|EMPLACEMENT LOCATION(3,1)|ENTIRE US ECONOMY(3,1)|EXCHANGE COEFFICIENT(3,1)|EXCHANGING RESIN(3,1)|EXPERIMENTAL WORK(3,1)|EXTANT FARM EQUIPMENT(3,1)|FILTRATE ANALYSIS(3,1)|FULL SUMMATION(3,1)|GRIND CELL(3,1)|HEAVY PHOSPHATE(3,1)|ICP ANALYSIS(3,1)|IMMOBILIZATION(3,1)|INDIGO CARBON(3,1)|LABORATORY SETTING(3,1)|MARINE SETTING(3,1)|MINERAL DELIVERY(3,1)|MINERAL DISSOLUTION RATE(3,1)|NATURAL ABUNDANCE CALCULATION(3,1)|NATURAL SOILS(3,1)|NEGATIVE EMISSION(3,1)|PHOSPHATE ZINC PRECIPITATE(3,1)|PLANT DEMAND(3,1)|PROJECT EVALUATION CRITERIA(3,1)|RELEVANT ION(3,1)|ROCK ELEMENTAL ANALYSIS(3,1)|ROCK MATERIAL ACCELERATED WEATHERING(3,1)|SAMPLING DENSITY(3,1)|SHARP THRESHOLD(3,1)|SLOW RELEASE ACIDIFIER(3,1)|SOIL ELEMENTAL ANALYSIS(3,1)|SUBSURFACE SOIL PORE WATER(3,1)|TECHNOLOGICAL SOLUTION(3,1)|WET GRAM(3,1)|ANALYTICAL CHEMISTRY(2,3)|LYSE(2,3)|4H4SIO(2,1)|ABILITY THRESHOLD(2,1)|ACCEPTANCE(2,1)|ACCOUNTING(2,1)|ACID TREATED ARTHROBACTER(2,1)|ACIDIC SOIL SOLUTION(2,1)|ADDITIONALITY(2,1)|ADMIXTURE(2,1)|AERATION(2,1)|AGLIME MESH SIZE OBSERVATION(2,1)|AGRICULTURE(2,1)|ALGAL BLOOM(2,1)|ANALYTICAL SOLUTION(2,1)|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)|ATTRACTION(2,1)|AUTOCLAVE(2,1)|BACTERIA(2,1)|BIOADSORBED METAL ACTIVE RELEASE(2,1)|BIOFUEL(2,1)|CA BEARING SILICATE(2,1)|CA CONTENT(2,1)|CALIBRATION STANDARD(2,1)|CAPTURING CARBON(2,1)|CATION EXCHANGE COLUMN(2,1)|CHARGE BALANCE(2,1)|CHELATOR(2,1)|CHITOSAN(2,1)|CLASSIFICATION(2,1)|CLAWBACK(2,1)|CLIMEWORK(2,1)|CO2 MOLECULAR MASS(2,1)|COMPACT MASS(2,1)|COMPREHENSIVE PROPOSAL NUMBER(2,1)||(US20220404329)|MINERAL AMENDMENT(100,30)|VERIFICATION(100,17)|REMOVING CARBON(100,13)|ENHANCED ROCK(100,8)|ENHANCED ROCK WEATHERING(100,3)|SILICATE MINERAL AGGLOMERATION(46,2)|COMMINUTED SILICATE MINERAL(39,3)|IMMOBILE TRACE ELEMENT(32,34)|INTERESTED PARTY(31,1)|FUNDAMENTAL ISSUE(25,1)|MINERAL TRANSFORMATION(21,2)|ETHYLENE DIAMINE TETRAACETIC ACID(20,1)|SAMPLING COLUMN(19,1)|CARBON MEASUREMENT OBJECTIVE(18,1)|IMMOBILE TRACE ELEMENT ABUNDANCE(16,1)|LANDOWNER(16,1)|SOIL SAMPLE(15,10)|SLOW RELEASE ACIDIFIER(15,3)|DIVALENT CATION MEASUREMENT(15,2)|BERYLLIUM(12,3)|VANADIUM(12,2)|COMMERCIAL ENTERPRISE(12,1)|DYSPROSIUM(11,10)|GADOLINIUM(11,8)|PRASEODYMIUM(11,7)|GERMANIUM(11,3)|RUBIDIUM(11,3)|ZIRCONIUM(11,3)|NEODYMIUM(10,12)|EUROPIUM(10,11)|LANTHANUM(10,10)|SAMARIUM(10,9)|SCANDIUM(10,9)|YTTERBIUM(10,9)|HOLMIUM(10,7)|LUTETIUM(10,7)|THULIUM(10,7)|BINDER(10,3)|GALLIUM(10,3)|HAFNIUM(10,3)|NIOBIUM(10,3)|TANTALUM(10,3)|GIBBSITE(10,2)|RARE METAL(9,6)|CESIUM(9,3)|CHROMIUM(9,3)|MINERAL AMENDMENT ADDITION(9,1)|CERIUM(8,10)|YTTRIUM(8,9)|BRUKER PROPRIETARY GEO CALIBRATION(8,1)|TRANSITION METAL(7,7)|DRAWDOWN CALCULATION(7,4)|VROCK MONTE CARLO SIMULATION(7,1)|AVERAGE PARTICLE SIZE(6,4)|ERW(6,4)|GYPSUM(6,3)|BLAST FURNACE SLAG(6,2)|CASO(6,2)|RIGOROUS QUANTIFICATION(6,2)|SIO2 PERCENT MINERALOGICAL FRACTION(6,2)|BIOLOGICAL DERIVED COMPONENT(6,1)|DELIVER PROSPECTIVE REWARD(6,1)|DIVERSE DECARBONIZATION STRATEGY(6,1)|PELLETIZED MINERAL AMENDMENT(6,1)|SCIENCE SUPPORTIVE ECOSYSTEM(6,1)|STERILIZED SOIL BEAKER(6,1)|RARE EARTH ELEMENT(5,20)|PPB DETECTION(5,4)|INSTRUMENTAL ERROR(5,3)|MINERAL SOIL AMENDMENT(5,3)|AIRTIGHT CONTAINMENT(5,2)|APPLIED DIVALENT CATION(5,2)|COMPUTING VROCK(5,2)|DISSOLUTION KINETICS(5,2)|NONLIMITING CANDIDATE(5,2)|PHOSPHATE FERTILIZER(5,2)|PULVERIZED SILICATE(5,2)|ALKALIZER KINETICS(5,1)|MINERAL ADDITIVE PROVEN IDENTITY(5,1)|SOIL ORGANIC CARBON(5,1)|TAXONOMY DISTINGUISHE(5,1)|UNINHABITABLE WATERWAY(5,1)|WET BIOMASS WET ALIQUOT(5,1)|CARBON FLUX(4,3)|CENTRIFUGE CELL(4,3)|CHARGE IMBALANCE(4,2)|INORGANIC ADDITIVE(4,2)|MG PPM DETECTION(4,2)|NEUTRAL GROUND(4,2)|ROCK PARTICLE(4,2)|VROCK DOT PRODUCT(4,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(4,1)|AGGREGATED PELLET(4,1)|AGLIME SUBSTITUTE(4,1)|AGRICULTURAL SOILS(4,1)|AGRONOMIC PERFORMANCE EXPECTATION(4,1)|ALKALINITY EXPORT(4,1)|BIODEGRADABLE TRANSPORTER(4,1)|BIOFILM MEDIATING(4,1)|CO2 REAGENT AVAILABILITY(4,1)|CO2 UPTAKE(4,1)|CUMULATIVE CATION FLUX MEASURE(4,1)|DDIC DTA ESTIMATE(4,1)|FORSTERITE METRIC TON(4,1)|FORSTERITE TENDENCY(4,1)|HENRY LAW COEFFICIENT(4,1)|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(4,1)|INFERRED ION FLUX(4,1)|INSTRUMENTAL UNCERTAINTY(4,1)|INTENSE SCRUTINY(4,1)|MARKETING COLLATERAL(4,1)|MICRONUTRIENT INCORPORATION(4,1)|MYCORRHIZAL INOCULUM(4,1)|NONPROFIT ORGANIZATION(4,1)|OCEAN ACIDIFICATION(4,1)|PELLET AGGLOMERATION(4,1)|PHOSPHORUS ECOSYSTEM LOSS(4,1)|PORTABLE XRF INSTRUMENT(4,1)|PREAPPLICATION SOIL(4,1)|PROTONATED MICROBE(4,1)|PULVERIZED LIMESTONE(4,1)|PULVERIZED MG2SIO(4,1)|RENOWNED CHEMIST(4,1)|RESPIRATORY HEALTH IMPACT(4,1)|REWET BIOMASS(4,1)|RIGOROUS COMPLIANCE(4,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)|SOIL CULTIVATED ZONE(4,1)|SOIL GEOCHEMISTRY(4,1)|SOIL HYDROLOGY(4,1)|X RAY FLUORESCENCE SPECTROSCOPY(4,1)|CARBON DIOXIDE REMOVAL(3,9)|NACL SOLUTION(3,4)|PROMETHIUM(3,4)|PULVERIZATION(3,4)|TRIPLICATE(3,4)|AQUEOUS CO2(3,2)|AVOIDED EMISSION(3,2)|BICARBONATE HCO3(3,2)|CARBONATE SPECIES(3,2)|DISSOLVED CARBONATE(3,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)|GROWING PLANT(3,2)|MINERAL POTENTIAL(3,2)|SECURE VESSEL(3,2)|SOIL ENVIRONMENT(3,2)|ABUNDANT CO2(3,1)|ACCELERATE TIMING(3,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)|AEROSOL SIZED PARTICLE(3,1)|AGGREGATING GROUND MINERAL(3,1)|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)|ANALYTICAL LABORATORY(3,1)|ANCIENT ROCK FORMATION(3,1)|ANION CONSERVATION(3,1)|AQUEOUS BICARBONATE MEASUREMENT(3,1)|AQUEOUS COMPLEXATION(3,1)|ASBESTOS EXPOSURE(3,1)|ASSEMBLING MP(3,1)|ATTENDANT DEMAND(3,1)|AUXILIARY GEOCHEMICAL DATA(3,1)|BICARBONATE MOLE(3,1)|BROAD FRAMEWORK(3,1)|CARBON EXCHANGE TRANSACTION(3,1)|CARBON VERIFICATION BENEFIT(3,1)|CATEGORY REGULATION(3,1)|CATION CONSERVATION(3,1)|CLAUSE XII(3,1)|COARSE PARTICLE(3,1)|COLLECT CELL PELLET(3,1)|CONTINENTAL COLLISION RELEASE(3,1)|CROP HEALTH(3,1)|DIFFERENCE VROCK VECTOR(3,1)|DIFFERENCE VSOIL VECTOR(3,1)|DISSOLUTION ENHANCING(3,1)|DISSOLVE ALGINATE(3,1)|DISSOLVED ALGINATE POWDER(3,1)|DIVALENT MG(3,1)|DOWNSTREAM ECOSYSTEM(3,1)|DOWNSTREAM WATERWAY(3,1)|DTA DH INVERSE(3,1)|DUST PREVALENCE(3,1)|ENHANCED ROCK FINANCIAL PERFORMANCE(3,1)|EQUILIBRIUM EQUATION(3,1)|FERTILIZATION FREQUENCY(3,1)|FRAUDULENT SAMPLE(3,1)|FUNGAL ADJUVANT(3,1)|GROUND MINERAL AGGREGATION(3,1)|GROUND NATURAL ENVIRONMENT(3,1)|H2CO SUM(3,1)|INCREASE ECOSYSTEM COBENEFIT(3,1)|KEY INSIGHT(3,1)|LB BROTH(3,1)|MICROBIAL CATION EXCHANGER(3,1)|MINERAL ADJUVANT(3,1)|MINERAL TRANSFORMATION EXTENT(3,1)|MINUS PROTON DONOR(3,1)|NUTRIENT AVAILABILITY(3,1)|PELLET DISSOLUTION(3,1)|PHOSPHATE LEACHING(3,1)|PHOSPHATE MOBILITY(3,1)|PRECISE ANSWER(3,1)|PREEQUILIBRATED TUBE(3,1)|PROGRESS FRACTIONATION(3,1)|QUASI GOVERNMENTAL REGULATOR(3,1)|REACTION THERMODYNAMICS(3,1)|RESERVOIR GEOLOGY(3,1)|SECURITIZED CARBON REMOVAL(3,1)|SILICATE MINERAL SHELL(3,1)|SILICATE ROLE(3,1)|SOIL STERILIZATION(3,1)|SPECIALIZED TOOL(3,1)|STEAM STERILIZATION(3,1)|TECHNO ECONOMIC MODELING(3,1)|ULTIMATE PRICE(3,1)|UNSEALING SAMPLE(3,1)|UREY REACTION BASIC PREMISE(3,1)|VERIFIABLE CARBON REMOVAL(3,1)|VERIFICATION VERSION(3,1)|VERIFIED ENHANCED ROCK(3,1)|VOLUNTARY MARKET(3,1)|XRF ANALYSIS(3,1)|ANALYTICAL CHEMISTRY(2,3)|LYSE(2,3)|BAG(2,2)|CO2 REMOVAL(2,2)|COMMINUTION(2,2)|FARMER(2,2)|MARKET ABILITY(2,2)|PELLETIZING(2,2)|PRODUCT FORMULATION(2,2)|STAKEHOLDER(2,2)|TOTAL FORMULATION(2,2)|ACIDIC ENVIRONMENT(2,1)|ANALYTICAL PERFORMANCE(2,1)|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)|CARBON MARKET MATURATION(2,1)|CARBON REMOVAL VERIFICATION(2,1)|CARBON TRANSACTION(2,1)|COMPUTING INDEX(2,1)|CORTEVA CARBON(2,1)|DRIED PELLET(2,1)|EMPLACEMENT LOCATION(2,1)|ENTIRE US ECONOMY(2,1)|EXCHANGE COEFFICIENT(2,1)|EXCHANGING RESIN(2,1)|EXPERIMENTAL WORK(2,1)|EXTANT FARM EQUIPMENT(2,1)|FILTRATE ANALYSIS(2,1)|FULL SUMMATION(2,1)|GRIND CELL(2,1)|HEAVY PHOSPHATE(2,1)|ICP ANALYSIS(2,1)|IMMOBILIZATION(2,1)|INDIGO CARBON(2,1)|LABORATORY SETTING(2,1)|MARINE SETTING(2,1)|MINERAL DELIVERY(2,1)|MINERAL DISSOLUTION RATE(2,1)|NATURAL ABUNDANCE CALCULATION(2,1)|NATURAL SOILS(2,1)|NEGATIVE EMISSION(2,1)|PHOSPHATE ZINC PRECIPITATE(2,1)|PLANT DEMAND(2,1)|PROJECT EVALUATION CRITERIA(2,1)|RELEVANT ION(2,1)|ROCK ELEMENTAL ANALYSIS(2,1)|ROCK MATERIAL ACCELERATED WEATHERING(2,1)|SAMPLING DENSITY(2,1)|SHARP THRESHOLD(2,1)|SOIL ELEMENTAL ANALYSIS(2,1)|SUBSURFACE SOIL PORE WATER(2,1)|TECHNOLOGICAL SOLUTION(2,1)|WET GRAM(2,1)|ABILITY THRESHOLD(1,1)|ACCEPTANCE(1,1)|ACCOUNTING(1,1)|ACID TREATED ARTHROBACTER(1,1)|ACIDIC SOIL SOLUTION(1,1)|ADDITIONALITY(1,1)|ADMIXTURE(1,1)|AERATION(1,1)|AGLIME MESH SIZE OBSERVATION(1,1)|AGRICULTURE(1,1)|ALGAL BLOOM(1,1)|ANALYTICAL SOLUTION(1,1)|APPLIED MINERAL AGRONOMIC BENEFIT(1,1)|ATTRACTION(1,1)|AUTOCLAVE(1,1)|BACTERIA(1,1)|BIOADSORBED METAL ACTIVE RELEASE(1,1)|BIOFUEL(1,1)|CA BEARING SILICATE(1,1)|CA CONTENT(1,1)|CALIBRATION STANDARD(1,1)|CAPTURING CARBON(1,1)|CATION EXCHANGE COLUMN(1,1)|CHARGE BALANCE(1,1)|CHELATOR(1,1)|CHITOSAN(1,1)|CLASSIFICATION(1,1)|CLAWBACK(1,1)|CLIMEWORK(1,1)||(US20260016458)|MINERAL AMENDMENT(100,20)|VERIFICATION(100,17)|REMOVING CARBON(100,12)|ENHANCED ROCK(100,7)|VERIFYING ENHANCED ROCK WEATHERING(70,1)|IMMOBILE TRACE ELEMENT(55,11)|ENHANCED ROCK WEATHERING(43,2)|INTERESTED PARTY(42,1)|RECOVERING SAMPLING COLUMN(36,1)|FUNDAMENTAL ISSUE(35,1)|CARBON MEASUREMENT OBJECTIVE(24,1)|IMMOBILE TRACE ELEMENT ABUNDANCE(22,1)|LANDOWNER(22,1)|SOIL SAMPLE(21,10)|DIVALENT CATION MEASUREMENT(20,2)|COMMERCIAL ENTERPRISE(16,1)|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)|MINERAL AMENDMENT ADDITION(12,1)|VANADIUM(12,1)|EUROPIUM(11,10)|DYSPROSIUM(11,9)|PRASEODYMIUM(11,6)|BRUKER PROPRIETARY GEO CALIBRATION(11,1)|LANTHANUM(10,9)|SAMARIUM(10,8)|SCANDIUM(10,8)|YTTERBIUM(10,8)|GADOLINIUM(10,7)|HOLMIUM(10,6)|LUTETIUM(10,6)|THULIUM(10,6)|BERYLLIUM(10,2)|GERMANIUM(10,2)|RUBIDIUM(10,2)|SIO PERCENT MINERALOGICAL FRACTION(10,2)|ZIRCONIUM(10,2)|DRAWDOWN CALCULATION(9,4)|ERW(9,4)|GALLIUM(9,2)|HAFNIUM(9,2)|NIOBIUM(9,2)|REES PPB DETECTION(9,2)|TANTALUM(9,2)|ANDTHE TRANSITION METAL(9,1)|DAC PROJECT RIGOROUS QUANTIFICATION(9,1)|CERIUM(8,9)|YTTRIUM(8,8)|RARE EARTH ELEMENT(8,6)|RARE METAL(8,4)|MINERAL SOIL AMENDMENT(8,3)|AIRTIGHT CONTAINMENT(8,2)|CESIUM(8,2)|CHROMIUM(8,2)|ETHYLENEDIAMINETETRAACETIC ACID(8,2)|NONLIMITING CANDIDATE(8,2)|REE TRIPLICATE(8,2)|CARBON DIOXIDE REMOVAL FRACTIONATION(8,1)|DELIVER PROSPECTIVE REWARD(8,1)|PELLETIZED MINERAL AMENDMENT(8,1)|SCIENCE SUPPORTIVE ECOSYSTEM(8,1)|STERILIZED SOIL BEAKER(8,1)|INSTRUMENTAL ERROR(7,3)|PHOSPHATE FERTILIZER(7,2)|ALKALIZER KINETICS(7,1)|DAC ULTIMATE PRICE(7,1)|MINERAL ADDITIVE PROVEN IDENTITY(7,1)|PHOSPHATE LEACHING LIKELIHOOD(7,1)|SOIL ORGANIC CARBON(7,1)|TAXONOMY DISTINGUISHE(7,1)|UNINHABITABLE WATERWAY(7,1)|WET BIOMASS WET ALIQUOT(7,1)|TRANSITION METAL(6,5)|CARBON FLUX(6,3)|APPLIED DIVALENT CATION(6,2)|CDR CALCULATION(6,2)|DISSOLUTION KINETICS(6,2)|PULVERIZED SILICATE(6,2)|ROCK PARTICLE(6,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)|ALKALINITY EXPORT(6,1)|BIODEGRADABLE TRANSPORTER(6,1)|CUMULATIVE CATION FLUX MEASURE(6,1)|FORSTERITE METRIC TON(6,1)|HENRY LAW COEFFICIENT(6,1)|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(6,1)|INSTRUMENTAL UNCERTAINTY(6,1)|ITE FINGERPRINT(6,1)|ITES ABUNDANCE(6,1)|MICRONUTRIENT INCORPORATION(6,1)|MYCORRHIZAL INOCULUM(6,1)|PELLET AGGLOMERATION(6,1)|PORTABLE XRF INSTRUMENT(6,1)|RESPIRATORY HEALTH IMPACT(6,1)|CENTRIFUGE CELL(5,3)|CHARGE IMBALANCE(5,2)|GROWING PLANT(5,2)|INORGANIC ADDITIVE(5,2)|MG PPM DETECTION(5,2)|NEUTRAL GROUND(5,2)|AGGREGATED PELLET(5,1)|AGLIME SUBSTITUTE(5,1)|AGRICULTURAL SOILS(5,1)|AGRONOMIC PERFORMANCE EXPECTATION(5,1)|BIOFILM MEDIATING(5,1)|DDIC DTA ESTIMATE(5,1)|DRAWDOWN ESTIMATION(5,1)|FORSTERITE TENDENCY(5,1)|INFERRED ION FLUX(5,1)|INTENSE SCRUTINY(5,1)|ITES PROPORTION(5,1)|MARKETING COLLATERAL(5,1)|NEGATIVELY CHARGED BICARBONATE(5,1)|NONPROFIT ORGANIZATION(5,1)|OCEAN ACIDIFICATION(5,1)|PHOSPHORUS ECOSYSTEM LOSS(5,1)|PREAPPLICATION SOIL(5,1)|PROTONATED MICROBE(5,1)|PULVERIZED LIMESTONE(5,1)|RENOWNED CHEMIST(5,1)|REWET BIOMASS(5,1)|RIGOROUS COMPLIANCE(5,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(5,1)|SOIL CULTIVATED ZONE(5,1)|SOIL GEOCHEMISTRY(5,1)|SOIL HYDROLOGY(5,1)|X RAY FLUORESCENCE SPECTROSCOPY(5,1)|NACL SOLUTION(4,4)|PROMETHIUM(4,4)|PULVERIZATION(4,4)|AVOIDED EMISSION(4,2)|CARBONATE DISSOLUTION(4,2)|CARBONATE SPECIES(4,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)|MARKET ABILITY(4,2)|MINERAL POTENTIAL(4,2)|SECURE VESSEL(4,2)|SOIL ENVIRONMENT(4,2)|ACCELERATE TIMING(4,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)|AEROSOL SIZED PARTICLE(4,1)|AGGREGATING GROUND MINERAL(4,1)|ANALYTICAL LABORATORY(4,1)|ANCIENT ROCK FORMATION(4,1)|ANION CONSERVATION(4,1)|ASBESTOS EXPOSURE(4,1)|ASSEMBLING MP(4,1)|ATTENDANT DEMAND(4,1)|AUXILIARY GEOCHEMICAL DATA(4,1)|BICARBONATE MOLE(4,1)|BROAD FRAMEWORK(4,1)|CARBON EXCHANGE TRANSACTION(4,1)|CARBON VERIFICATION BENEFIT(4,1)|CATEGORY REGULATION(4,1)|CATION CONSERVATION(4,1)|CLAUSE XII(4,1)|COARSE PARTICLE(4,1)|COLLECT CELL PELLET(4,1)|CONTINENTAL COLLISION RELEASE(4,1)|CROP HEALTH(4,1)|CUSTOM ITE STANDARD(4,1)|DISSOLUTION ENHANCING(4,1)|DISSOLVE ALGINATE(4,1)|DISSOLVED ALGINATE(4,1)|DIVALENT MG(4,1)|DOWNSTREAM ECOSYSTEM(4,1)|DOWNSTREAM WATERWAY(4,1)|DTA DH INVERSE(4,1)|DUST PREVALENCE(4,1)|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)|EQUILIBRIUM EQUATION(4,1)|FERTILIZATION FREQUENCY(4,1)|FRAUDULENT SAMPLE(4,1)|FUNGAL ADJUVANT(4,1)|GROUND MINERAL AGGREGATION(4,1)|GROUND NATURAL ENVIRONMENT(4,1)|HEAVY PHOSPHATE(4,1)|HEAVY REES(4,1)|INCREASE ECOSYSTEM COBENEFIT(4,1)|KEY INSIGHT(4,1)|LB BROTH(4,1)|MICROBIAL CATION EXCHANGER(4,1)|MINERAL ADJUVANT(4,1)|MINERAL TON HECTARE(4,1)|MINERAL TRANSFORMATION EXTENT(4,1)|MINUS PROTON DONOR(4,1)|NATIVE ITE(4,1)|NUTRIENT AVAILABILITY(4,1)|PELLET DISSOLUTION(4,1)|PHOSPHATE MOBILITY(4,1)|PPM NEODYMIUM(4,1)|PRECISE ANSWER(4,1)|PREEQUILIBRATED TUBE(4,1)|PROGRESS FRACTIONATION(4,1)|PULVERIZED MG(4,1)|QUASI GOVERNMENTAL REGULATOR(4,1)|REACTION THERMODYNAMICS(4,1)|REE AQUEOUS COMPLEXATION(4,1)|REES FULL RECOVERY(4,1)|RESERVOIR GEOLOGY(4,1)|SILICATE MINERAL SHELL(4,1)|SILICATE ROLE(4,1)|SOIL STERILIZATION(4,1)|SPECIALIZED TOOL(4,1)|STEAM STERILIZATION(4,1)|TECHNICAL CDR(4,1)|TECHNO ECONOMIC MODELING(4,1)|UNSEALING SAMPLE(4,1)|UREY REACTION BASIC PREMISE(4,1)|V MONTE CARLO SIMULATION(4,1)|VERIFIABLE CARBON REMOVAL(4,1)|VERIFICATION VERSION(4,1)|VERIFIED ENHANCED ROCK(4,1)|VOLUNTARY MARKET(4,1)|XRF ANALYSIS(4,1)|HCO(3,4)|K2H(3,4)|BAG(3,2)|BINDER(3,2)|COMMINUTION(3,2)|FARMER(3,2)|PELLETIZING(3,2)|PRODUCT FORMULATION(3,2)|STAKEHOLDER(3,2)|TOTAL FORMULATION(3,2)|ACIDIC ENVIRONMENT(3,1)|ANALYTICAL PERFORMANCE(3,1)|AQUEOUS BICARBONATE(3,1)|CARBON MARKET MATURATION(3,1)|CARBON REMOVAL VERIFICATION(3,1)|CARBON TRANSACTION(3,1)|COMPUTING INDEX(3,1)|CORTEVA CARBON(3,1)|DRIED PELLET(3,1)|EMPLACEMENT LOCATION(3,1)|ENTIRE US ECONOMY(3,1)|EXCHANGE COEFFICIENT(3,1)|EXCHANGING RESIN(3,1)|EXPERIMENTAL WORK(3,1)|EXTANT FARM EQUIPMENT(3,1)|FILTRATE ANALYSIS(3,1)|FULL SUMMATION(3,1)|GRIND CELL(3,1)|ICP ANALYSIS(3,1)|IMMOBILIZATION(3,1)|INDIGO CARBON(3,1)|ITES COST(3,1)|LABORATORY SETTING(3,1)|MARINE SETTING(3,1)|MINERAL DELIVERY(3,1)|MINERAL DISSOLUTION RATE(3,1)|NATURAL ABUNDANCE CALCULATION(3,1)|NATURAL SOILS(3,1)|NEGATIVE EMISSION(3,1)|PHOSPHATE ZINC PRECIPITATE(3,1)|PLANT DEMAND(3,1)|PROJECT EVALUATION CRITERIA(3,1)|RELEVANT ION(3,1)|ROCK ELEMENTAL ANALYSIS(3,1)|ROCK MATERIAL ACCELERATED WEATHERING(3,1)|SAMPLING DENSITY(3,1)|SHARP THRESHOLD(3,1)|SLOW RELEASE ACIDIFIER(3,1)|SOIL ELEMENTAL ANALYSIS(3,1)|SUBSURFACE SOIL PORE WATER(3,1)|TECHNOLOGICAL SOLUTION(3,1)|WET GRAM(3,1)|ANALYTICAL CHEMISTRY(2,3)|K1H(2,3)|LYSE(2,3)|ABILITY THRESHOLD(2,1)|ACCEPTANCE(2,1)|ACCOUNTING(2,1)|ACID TREATED ARTHROBACTER(2,1)|ACIDIC SOIL SOLUTION(2,1)|ADDITIONALITY(2,1)|ADMIXTURE(2,1)|AERATION(2,1)|AGLIME MESH SIZE OBSERVATION(2,1)|AGRICULTURE(2,1)|ALGAL BLOOM(2,1)|ANALYTICAL SOLUTION(2,1)|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)|ATTRACTION(2,1)|AUTOCLAVE(2,1)|BACTERIA(2,1)|BIOADSORBED METAL ACTIVE RELEASE(2,1)|BIOFUEL(2,1)|CA BEARING SILICATE(2,1)|CA CONTENT(2,1)|CALIBRATION STANDARD(2,1)|CAPTURING CARBON(2,1)|CATION EXCHANGE COLUMN(2,1)|CHARGE BALANCE(2,1)|CHELATOR(2,1)|CHITOSAN(2,1)|CLASSIFICATION(2,1)|CLAWBACK(2,1)|CLIMEWORK(2,1)|COMPACT MASS(2,1)|COMPREHENSIVE PROPOSAL NUMBER(2,1)||(WO2022/271842)|MINERAL AMENDMENT(100,30)|VERIFICATION(100,19)|REMOVING CARBON(100,14)|ENHANCED ROCK(100,10)|ENHANCED ROCK WEATHERING(100,3)|SILICATE MINERAL AGGLOMERATION(46,2)|COMMINUTED SILICATE MINERAL(39,3)|IMMOBILE TRACE ELEMENT(32,34)|INTERESTED PARTY(31,1)|FUNDAMENTAL ISSUE(25,1)|SAMPLING COLUMN(19,1)|CARBON MEASUREMENT OBJECTIVE(18,1)|IMMOBILE TRACE ELEMENT ABUNDANCE(16,1)|LANDOWNER(16,1)|SOIL SAMPLE(15,10)|SLOW RELEASE ACIDIFIER(15,3)|DIVALENT CATION MEASUREMENT(15,2)|BERYLLIUM(12,3)|VANADIUM(12,2)|COMMERCIAL ENTERPRISE(12,1)|DYSPROSIUM(11,10)|GADOLINIUM(11,8)|PRASEODYMIUM(11,7)|GERMANIUM(11,3)|RUBIDIUM(11,3)|ZIRCONIUM(11,3)|NEODYMIUM(10,12)|EUROPIUM(10,11)|LANTHANUM(10,10)|SAMARIUM(10,9)|SCANDIUM(10,9)|YTTERBIUM(10,9)|HOLMIUM(10,7)|LUTETIUM(10,7)|THULIUM(10,7)|BINDER(10,3)|GALLIUM(10,3)|HAFNIUM(10,3)|NIOBIUM(10,3)|TANTALUM(10,3)|GIBBSITE(10,2)|RARE METAL(9,6)|CESIUM(9,3)|CHROMIUM(9,3)|MINERAL AMENDMENT ADDITION(9,1)|CERIUM(8,10)|YTTRIUM(8,9)|BRUKER PROPRIETARY GEO CALIBRATION(8,1)|TRANSITION METAL(7,7)|DRAWDOWN CALCULATION(7,4)|ETHYLENEDIAMINETETRAACETIC ACID(7,1)|VR0CK MONTE CARLO SIMULATION(7,1)|AVERAGE PARTICLE SIZE(6,4)|ERW(6,4)|GYPSUM(6,3)|MINERAL SOIL AMENDMENT(6,3)|BLAST FURNACE SLAG(6,2)|RIGOROUS QUANTIFICATION(6,2)|BIOLOGICAL DERIVED COMPONENT(6,1)|DDIC DH DTA(6,1)|DELIVER PROSPECTIVE REWARD(6,1)|DIVERSE DECARBONIZATION STRATEGY(6,1)|PELLETIZED MINERAL AMENDMENT(6,1)|SCIENCE SUPPORTIVE ECOSYSTEM(6,1)|STERILIZED SOIL BEAKER(6,1)|RARE EARTH ELEMENT(5,20)|PPB DETECTION(5,4)|INSTRUMENTAL ERROR(5,3)|AIRTIGHT CONTAINMENT(5,2)|APPLIED DIVALENT CATION(5,2)|COMPUTING VROCK(5,2)|DISSOLUTION KINETICS(5,2)|NONLIMITING CANDIDATE(5,2)|PHOSPHATE FERTILIZER(5,2)|PULVERIZED SILICATE(5,2)|SI PERCENT MINERALOGICAL FRACTION(5,2)|ALKALIZER KINETICS(5,1)|MINERAL ADDITIVE PROVEN IDENTITY(5,1)|SOIL ORGANIC CARBON(5,1)|TAXONOMY DISTINGUISHE(5,1)|UNINHABITABLE WATERWAY(5,1)|WET BIOMASS WET ALIQUOT(5,1)|CARBON FLUX(4,3)|CENTRIFUGE CELL(4,3)|CHARGE IMBALANCE(4,2)|INORGANIC ADDITIVE(4,2)|MG PPM DETECTION(4,2)|NEUTRAL GROUND(4,2)|ROCK PARTICLE(4,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(4,1)|AGGREGATED PELLET(4,1)|AGLIME SUBSTITUTE(4,1)|AGRICULTURAL SOILS(4,1)|AGRONOMIC PERFORMANCE EXPECTATION(4,1)|ALKALINITY EXPORT(4,1)|BIODEGRADABLE TRANSPORTER(4,1)|BIOFILM MEDIATING(4,1)|CO2 REAGENT AVAILABILITY(4,1)|CO2 UPTAKE(4,1)|CUMULATIVE CATION FLUX MEASURE(4,1)|DDIC DTA ESTIMATE(4,1)|DRAWDOWN ESTIMATION(4,1)|FORSTERITE METRIC TON(4,1)|FORSTERITE TENDENCY(4,1)|HENRY LAW COEFFICIENT(4,1)|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(4,1)|INFERRED ION FLUX(4,1)|INSTRUMENTAL UNCERTAINTY(4,1)|INTENSE SCRUTINY(4,1)|MARKETING COLLATERAL(4,1)|MICRONUTRIENT INCORPORATION(4,1)|MYCORRHIZAL INOCULUM(4,1)|NEGATIVELY CHARGED BICARBONATE(4,1)|NONPROFIT ORGANIZATION(4,1)|OCEAN ACIDIFICATION(4,1)|PELLET AGGLOMERATION(4,1)|PHOSPHORUS ECOSYSTEM LOSS(4,1)|PORTABLE XRF INSTRUMENT(4,1)|PREAPPLICATION SOIL(4,1)|PROTONATED MICROBE(4,1)|PULVERIZED LIMESTONE(4,1)|PULVERIZED MGISICE(4,1)|RENOWNED CHEMIST(4,1)|RESPIRATORY HEALTH IMPACT(4,1)|REWET BIOMASS(4,1)|RIGOROUS COMPLIANCE(4,1)|RLE TRIPLICATE(4,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)|SOIL CULTIVATED ZONE(4,1)|SOIL GEOCHEMISTRY(4,1)|SOIL HYDROLOGY(4,1)|X RAY FLUORESCENCE SPECTROSCOPY(4,1)|CARBON DIOXIDE REMOVAL(3,9)|NACL SOLUTION(3,4)|PROMETHIUM(3,4)|PULVERIZATION(3,4)|AQUEOUS CO2(3,2)|AVOIDED EMISSION(3,2)|CARBONATE SPECIES(3,2)|DISSOLVED CARBONATE(3,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)|GROWING PLANT(3,2)|MINERAL POTENTIAL(3,2)|SECURE VESSEL(3,2)|SOIL ENVIRONMENT(3,2)|ACCELERATE TIMING(3,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)|AEROSOL SIZED PARTICLE(3,1)|AGGREGATING GROUND MINERAL(3,1)|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)|ANALYTICAL LABORATORY(3,1)|ANCIENT ROCK FORMATION(3,1)|ANION CONSERVATION(3,1)|AQUEOUS BICARBONATE MEASUREMENT(3,1)|AQUEOUS COMPLEXATION(3,1)|ASBESTOS EXPOSURE(3,1)|ASSEMBLING MP(3,1)|ATTENDANT DEMAND(3,1)|AUXILIARY GEOCHEMICAL DATA(3,1)|BICARBONATE MOLE(3,1)|BROAD FRAMEWORK(3,1)|CARBON EXCHANGE TRANSACTION(3,1)|CARBON VERIFICATION BENEFIT(3,1)|CATEGORY REGULATION(3,1)|CATION CONSERVATION(3,1)|CLAUSE XII(3,1)|COARSE PARTICLE(3,1)|CONTINENTAL COLLISION RELEASE(3,1)|CROP HEALTH(3,1)|DIFFERENCE VR0CK VECTOR(3,1)|DIFFERENCE VSOU VECTOR(3,1)|DISSOLUTION ENHANCING(3,1)|DISSOLVE ALGINATE(3,1)|DISSOLVED ALGINATE POWDER(3,1)|DIVALENT MG(3,1)|DOWNSTREAM ECOSYSTEM(3,1)|DOWNSTREAM WATERWAY(3,1)|DTA DH INVERSE(3,1)|DUST PREVALENCE(3,1)|ECOSYSTEM CO BENEFIT(3,1)|EQUILIBRIUM EQUATION(3,1)|FERTILIZATION FREQUENCY(3,1)|FRAUDULENT SAMPLE(3,1)|FUNGAL ADJUVANT(3,1)|GROUND MINERAL AGGREGATION(3,1)|GROUND NATURAL ENVIRONMENT(3,1)|H2CO SUM(3,1)|INCREASE ECOSYSTEM COBENEFIT(3,1)|KEY INSIGHT(3,1)|LB BROTH(3,1)|MICROBIAL CATION EXCHANGER(3,1)|MINERAL ADJUVANT(3,1)|MINERAL TRANSFORMATION EXTENT(3,1)|MINUS PROTON DONOR(3,1)|NUTRIENT AVAILABILITY(3,1)|PELLET DISSOLUTION(3,1)|PHOSPHATE LEACHING(3,1)|PHOSPHATE MOBILITY(3,1)|PRECISE ANSWER(3,1)|PREEQUILIBRATED TUBE(3,1)|PROGRESS FRACTIONATION(3,1)|QUASI GOVERNMENTAL REGULATOR(3,1)|REACTION THERMODYNAMICS(3,1)|RESERVOIR GEOLOGY(3,1)|SECURITIZED CARBON REMOVAL(3,1)|SILICATE MINERAL SHELL(3,1)|SILICATE ROLE(3,1)|SOIL STERILIZATION(3,1)|SPECIALIZED TOOL(3,1)|STEAM STERILIZATION(3,1)|STYRENE DIVINYLBENZENE(3,1)|TECHNO ECONOMIC MODELING(3,1)|TREATMENT UNIFORMITY(3,1)|ULTIMATE PRICE(3,1)|UNSEALING SAMPLE(3,1)|UREY REACTION BASIC PREMISE(3,1)|VERIFIABLE CARBON REMOVAL(3,1)|VERIFICATION VERSION(3,1)|VERIFIED ENHANCED ROCK(3,1)|VOLUNTARY MARKET(3,1)|VROCK DOT PRODUCT(3,1)|XRF ANALYSIS(3,1)|ANALYTICAL CHEMISTRY(2,3)|LYSE(2,3)|BAG(2,2)|CO2 REMOVAL(2,2)|FARMER(2,2)|MARKET ABILITY(2,2)|PELLETIZING(2,2)|PRODUCT FORMULATION(2,2)|STAKEHOLDER(2,2)|TOTAL FORMULATION(2,2)|ACIDIC ENVIRONMENT(2,1)|ANALYTICAL PERFORMANCE(2,1)|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)|CARBON MARKET MATURATION(2,1)|CARBON REMOVAL VERIFICATION(2,1)|CARBON TRANSACTION(2,1)|CELL PELLET(2,1)|COMPUTING INDEX(2,1)|CORTEVA CARBON(2,1)|DRIED PELLET(2,1)|EMPLACEMENT LOCATION(2,1)|ENHANCED ROCK VARIABLE PERFORMANCE(2,1)|ENTIRE US ECONOMY(2,1)|EXCHANGE COEFFICIENT(2,1)|EXCHANGING RESIN(2,1)|EXPERIMENTAL WORK(2,1)|EXTANT FARM EQUIPMENT(2,1)|FILTRATE ANALYSIS(2,1)|FULL SUMMATION(2,1)|GRIND CELL(2,1)|HEAVY PHOSPHATE(2,1)|ICP ANALYSIS(2,1)|IMMOBILIZATION(2,1)|INDIGO CARBON(2,1)|LABORATORY SETTING(2,1)|MARINE SETTING(2,1)|MINERAL DELIVERY(2,1)|MINERAL DISSOLUTION RATE(2,1)|NATURAL ABUNDANCE CALCULATION(2,1)|NATURAL SOILS(2,1)|NEGATIVE EMISSION(2,1)|PHOSPHATE ZINC PRECIPITATE(2,1)|PLANT DEMAND(2,1)|PROJECT EVALUATION CRITERIA(2,1)|RELEVANT ION(2,1)|ROCK ELEMENTAL ANALYSIS(2,1)|ROCK MATERIAL ACCELERATED WEATHERING(2,1)|SAMPLING DENSITY(2,1)|SHARP THRESHOLD(2,1)|SOIL ELEMENTAL ANALYSIS(2,1)|SUBSURFACE SOIL PORE WATER(2,1)|TECHNOLOGICAL SOLUTION(2,1)|WET GRAM(2,1)|ABILITY THRESHOLD(1,1)|ACCEPTANCE(1,1)|ACCOUNTING(1,1)|ACID TREATED ARTHROBACTER(1,1)|ACIDIC SOIL SOLUTION(1,1)|ADDITIONALITY(1,1)|ADMIXTURE(1,1)|AERATION(1,1)|AGLIME MESH SIZE OBSERVATION(1,1)|AGRICULTURE(1,1)|ALGAL BLOOM(1,1)|ANALYTICAL SOLUTION(1,1)|APPLIED MINERAL AGRONOMIC BENEFIT(1,1)|ARACTUAI(1,1)|ATTRACTION(1,1)|AUTOCLAVE(1,1)|BACTERIA(1,1)|BIOADSORBED METAL ACTIVE RELEASE(1,1)|BIOFUEL(1,1)|CA BEARING SILICATE(1,1)|CA CONTENT(1,1)|CALIBRATION STANDARD(1,1)|CAPTURING CARBON(1,1)|CATION EXCHANGE COLUMN(1,1)|CHARGE BALANCE(1,1)|CHELATOR(1,1)|CHITOSAN(1,1)|CLASSIFICATION(1,1)|CLAWBACK(1,1)|CLIMEWORK(1,1)|CO2 MOLECULAR MASS(1,1)||(CA3207124)|MINERAL AMENDMENT(100,28)|ENHANCED ROCK(100,8)|ENHANCED ROCK WEATHERING(100,2)|SILICATE MINERAL AGGLOMERATION(51,2)|COMMINUTED SILICATE MINERAL(44,3)|INTERESTED PARTY(34,1)|IMMOBILE TRACE ELEMENT(33,33)|FUNDAMENTAL ISSUE(28,1)|MINERAL TRANSFORMATION(24,2)|ETHYLENE DIAMINE TETRAACETIC ACID(22,1)|SAMPLING COLUMN(21,1)|CARBON MEASUREMENT OBJECTIVE(20,1)|IMMOBILE TRACE ELEMENT ABUNDANCE(18,1)|LANDOWNER(18,1)|SOIL SAMPLE(17,10)|SLOW RELEASE ACIDIFIER(17,3)|DIVALENT CATION MEASUREMENT(17,2)|VERIFICATION(14,18)|VANADIUM(14,2)|BERYLLIUM(13,3)|COMMERCIAL ENTERPRISE(13,1)|DYSPROSIUM(12,10)|GADOLINIUM(12,8)|PRASEODYMIUM(12,7)|GERMANIUM(12,3)|RUBIDIUM(12,3)|ZIRCONIUM(12,3)|NEODYMIUM(11,12)|EUROPIUM(11,11)|LANTHANUM(11,10)|SAMARIUM(11,9)|SCANDIUM(11,9)|YTTERBIUM(11,9)|HOLMIUM(11,7)|LUTETIUM(11,7)|THULIUM(11,7)|BINDER(11,3)|GALLIUM(11,3)|HAFNIUM(11,3)|NIOBIUM(11,3)|TANTALUM(11,3)|GIBBSITE(11,2)|RARE METAL(10,6)|CESIUM(10,3)|CHROMIUM(10,3)|MINERAL AMENDMENT ADDITION(10,1)|CERIUM(9,10)|YTTRIUM(9,9)|BRUKER PROPRIETARY GEO CALIBRATION(9,1)|REMOVING CARBON(8,13)|TRANSITION METAL(8,7)|DRAWDOWN CALCULATION(8,4)|VROCK MONTE CARLO SIMULATION(8,1)|AVERAGE PARTICLE SIZE(7,4)|ERW(7,4)|BLAST FURNACE SLAG(7,2)|CASO(7,2)|RIGOROUS QUANTIFICATION(7,2)|BIOLOGICAL DERIVED COMPONENT(7,1)|DIVERSE DECARBONIZATION STRATEGY(7,1)|PELLETIZED MINERAL AMENDMENT(7,1)|SCIENCE SUPPORTIVE ECOSYSTEM(7,1)|RARE EARTH ELEMENT(6,20)|PPB DETECTION(6,4)|GYPSUM(6,3)|MINERAL SOIL AMENDMENT(6,3)|AIRTIGHT CONTAINMENT(6,2)|NONLIMITING CANDIDATE(6,2)|PHOSPHATE FERTILIZER(6,2)|SI PERCENT MINERALOGICAL FRACTION(6,2)|ALKALIZER KINETICS(6,1)|DELIVER PROSPECTIVE REWARD(6,1)|MINERAL ADDITIVE PROVEN IDENTITY(6,1)|NEGATIVELY CHARGED BICARBONATE HCO(6,1)|SOIL ORGANIC CARBON(6,1)|STERILIZED SOIL BEAKER(6,1)|TAXONOMY DISTINGUISHE(6,1)|UNINHABITABLE WATERWAY(6,1)|WET BIOMASS WET ALIQUOT(6,1)|CARBON FLUX(5,3)|INSTRUMENTAL ERROR(5,3)|APPLIED DIVALENT CATION(5,2)|COMPUTING VROCK(5,2)|DISSOLUTION KINETICS(5,2)|PULVERIZED SILICATE(5,2)|ROCK PARTICLE(5,2)|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(5,1)|ALKALINITY EXPORT(5,1)|BIODEGRADABLE TRANSPORTER(5,1)|CO2 REAGENT AVAILABILITY(5,1)|CUMULATIVE CATION FLUX MEASURE(5,1)|HENRY LAW COEFFICIENT(5,1)|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(5,1)|INSTRUMENTAL UNCERTAINTY(5,1)|MICRONUTRIENT INCORPORATION(5,1)|MYCORRHIZAL INOCULUM(5,1)|PELLET AGGLOMERATION(5,1)|PORTABLE XRF INSTRUMENT(5,1)|RESPIRATORY HEALTH IMPACT(5,1)|NACL SOLUTION(4,4)|PROMETHIUM(4,4)|PULVERIZATION(4,4)|TRIPLICATE(4,4)|CENTRIFUGE CELL(4,3)|CHARGE IMBALANCE(4,2)|GROWING PLANT(4,2)|INORGANIC ADDITIVE(4,2)|MG PPM DETECTION(4,2)|NEUTRAL GROUND(4,2)|VROCK DOT PRODUCT(4,2)|AEROSOL SIZED PARTICLE(4,1)|AGGREGATED PELLET(4,1)|AGGREGATING GROUND MINERAL(4,1)|AGLIME SUBSTITUTE(4,1)|AGRICULTURAL SOILS(4,1)|AGRONOMIC PERFORMANCE EXPECTATION(4,1)|ANALYTICAL LABORATORY(4,1)|ANCIENT ROCK FORMATION(4,1)|ANION CONSERVATION(4,1)|BIOFILM MEDIATING(4,1)|CATEGORY REGULATION(4,1)|CATION CONSERVATION(4,1)|CLAUSE XII(4,1)|CO2 UPTAKE(4,1)|DDIC DTA ESTIMATE(4,1)|DIFFERENCE VROCK VECTOR(4,1)|DISSOLVE ALGINATE(4,1)|DISSOLVED ALGINATE POWDER(4,1)|DOWNSTREAM ECOSYSTEM(4,1)|DOWNSTREAM WATERWAY(4,1)|DTA DH INVERSE(4,1)|DUST PREVALENCE(4,1)|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)|FORSTERITE MOLE(4,1)|FORSTERITE TENDENCY(4,1)|FUNGAL ADJUVANT(4,1)|GROUND MINERAL AGGREGATION(4,1)|INFERRED ION FLUX(4,1)|INTENSE SCRUTINY(4,1)|KEY INSIGHT(4,1)|MARKETING COLLATERAL(4,1)|MICROBIAL CATION EXCHANGER(4,1)|MINERAL ADJUVANT(4,1)|NONPROFIT ORGANIZATION(4,1)|NUTRIENT AVAILABILITY(4,1)|OCEAN ACIDIFICATION(4,1)|PELLET DISSOLUTION(4,1)|PHOSPHATE ZINC PRECIPITATE(4,1)|PHOSPHORUS ECOSYSTEM LOSS(4,1)|PREAPPLICATION SOIL(4,1)|PROGRESS FRACTIONATION(4,1)|PROTONATED MICROBE(4,1)|PULVERIZED LIMESTONE(4,1)|PULVERIZED MG2SIO(4,1)|QUASI GOVERNMENTAL REGULATOR(4,1)|RENOWNED CHEMIST(4,1)|RESERVOIR GEOLOGY(4,1)|REWET BIOMASS(4,1)|RIGOROUS COMPLIANCE(4,1)|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)|SOIL CULTIVATED ZONE(4,1)|SOIL GEOCHEMISTRY(4,1)|SOIL HYDROLOGY(4,1)|SOIL STERILIZATION(4,1)|SPECIALIZED TOOL(4,1)|STEAM STERILIZATION(4,1)|STYRENE DIVINYLBENZENE(4,1)|TECHNO ECONOMIC MODELING(4,1)|ULTIMATE PRICE(4,1)|UREY REACTION BASIC PREMISE(4,1)|VERIFICATION VERSION(4,1)|VERIFIED ENHANCED ROCK(4,1)|VOLUNTARY MARKET(4,1)|X RAY FLUORESCENCE SPECTROSCOPY(4,1)|CARBON DIOXIDE REMOVAL(3,10)|AQUEOUS CO2(3,2)|AVOIDED EMISSION(3,2)|CARBONATE SPECIES(3,2)|DISSOLVED CARBONATE(3,2)|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)|MARKET ABILITY(3,2)|SECURE VESSEL(3,2)|SOIL ENVIRONMENT(3,2)|ABUNDANT CO2(3,1)|ACCELERATE TIMING(3,1)|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)|AQUEOUS BICARBONATE MEASUREMENT(3,1)|AQUEOUS COMPLEXATION(3,1)|ASBESTOS EXPOSURE(3,1)|ASSEMBLING MP(3,1)|ATTENDANT DEMAND(3,1)|AUXILIARY GEOCHEMICAL DATA(3,1)|BICARBONATE MOLE(3,1)|BROAD FRAMEWORK(3,1)|CARBON EXCHANGE TRANSACTION(3,1)|CARBON VERIFICATION BENEFIT(3,1)|COARSE PARTICLE(3,1)|COLLECT CELL PELLET(3,1)|CONTINENTAL COLLISION RELEASE(3,1)|CROP HEALTH(3,1)|DISSOLUTION ENHANCING(3,1)|DIVALENT MG(3,1)|EQUILIBRIUM EQUATION(3,1)|FERTILIZATION FREQUENCY(3,1)|FRAUDULENT SAMPLE(3,1)|GROUND NATURAL ENVIRONMENT(3,1)|H2CO SUM(3,1)|INCREASE ECOSYSTEM COBENEFIT(3,1)|LB BROTH(3,1)|MINERAL TRANSFORMATION EXTENT(3,1)|MINUS PROTON DONOR(3,1)|PHOSPHATE LEACHING(3,1)|PHOSPHATE MOBILITY(3,1)|PRECISE ANSWER(3,1)|PREEQUILIBRATED TUBE(3,1)|REACTION THERMODYNAMICS(3,1)|SECURITIZED CARBON REMOVAL(3,1)|SILICATE MINERAL SHELL(3,1)|SILICATE ROLE(3,1)|UNSEALING SAMPLE(3,1)|VERIFIABLE CARBON REMOVAL(3,1)|XRF ANALYSIS(3,1)|ANALYTICAL CHEMISTRY(2,3)|LYSE(2,3)|VSOIT(2,3)|BAG(2,2)|CO2 REMOVAL(2,2)|FARMER(2,2)|PELLETIZING(2,2)|PRODUCT FORMULATION(2,2)|STAKEHOLDER(2,2)|TOTAL FORMULATION(2,2)|ABILITY THRESHOLD(2,1)|ACCEPTANCE(2,1)|ACCOUNTING(2,1)|ACID TREATED ARTHROBACTER(2,1)|ACIDIC ENVIRONMENT(2,1)|ACIDIC SOIL SOLUTION(2,1)|ADDITIONALITY(2,1)|ADMIXTURE(2,1)|AERATION(2,1)|AGLIME MESH SIZE OBSERVATION(2,1)|AGRICULTURE(2,1)|ALGAL BLOOM(2,1)|ANALYTICAL PERFORMANCE(2,1)|ANALYTICAL SOLUTION(2,1)|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)|ATTRACTION(2,1)|AUTOCLAVE(2,1)|BACTERIA(2,1)|BIOADSORBED METAL ACTIVE RELEASE(2,1)|BIOFUEL(2,1)|CA BEARING SILICATE(2,1)|CA CONTENT(2,1)|CALIBRATION STANDARD(2,1)|CAPTURING CARBON(2,1)|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)|CARBON MARKET MATURATION(2,1)|CARBON REMOVAL VERIFICATION(2,1)|CARBON TRANSACTION(2,1)|CATION EXCHANGE COLUMN(2,1)|CHARGE BALANCE(2,1)|CHELATOR(2,1)|CHITOSAN(2,1)|CLASSIFICATION(2,1)|COMPUTING INDEX(2,1)|CORTEVA CARBON(2,1)|DRIED PELLET(2,1)|EMPLACEMENT LOCATION(2,1)|ENTIRE US ECONOMY(2,1)|EXCHANGE COEFFICIENT(2,1)|EXCHANGING RESIN(2,1)|EXPERIMENTAL WORK(2,1)|EXTANT FARM EQUIPMENT(2,1)|FILTRATE ANALYSIS(2,1)|FULL SUMMATION(2,1)|GRIND CELL(2,1)|HEAVY PHOSPHATE(2,1)|ICP ANALYSIS(2,1)|IMMOBILIZATION(2,1)|INDIGO CARBON(2,1)|LABORATORY SETTING(2,1)|MARINE SETTING(2,1)|MINERAL DELIVERY(2,1)|MINERAL DISSOLUTION RATE(2,1)|MINERAL POTENTIAL(2,1)|NATURAL ABUNDANCE CALCULATION(2,1)|NATURAL SOILS(2,1)|NEGATIVE EMISSION(2,1)|PLANT DEMAND(2,1)|PROJECT EVALUATION CRITERIA(2,1)|RELEVANT ION(2,1)|ROCK ELEMENTAL ANALYSIS(2,1)|ROCK MATERIAL ACCELERATED WEATHERING(2,1)|SAMPLING DENSITY(2,1)|SHARP THRESHOLD(2,1)|SOIL ELEMENTAL ANALYSIS(2,1)|SUBSURFACE SOIL PORE WATER(2,1)|TECHNOLOGICAL SOLUTION(2,1)|WET GRAM(2,1)| (EP4256520)|1. A method for verifying enhanced rock weathering using a mineral amendment comprising:| measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and| subsequently measuring the immobile trace elements in a soil sample after application of the mineral amendment to verify application of the mineral amendment,| characterized in that the method comprises the steps of:| determining the amount of the mineral amendment added to the soil sample,| determining the amount of measured divalent cations in the soil sample,| determining the fractional carbon dioxide removal by comparing the applied divalent cations to the measured divalent cations in the soil sample.|2. The method of claim 1, wherein the immobile trace elements and magnesium are measured using inductively coupled plasma spectroscopy or x-ray fluorescence spectroscopy.|3. The method of claim 1, further comprising the step of measuring the immobile trace elements in the soil sample prior to addition of the mineral amendment.|4. The method of claim 1, further comprising the step of enriching the abundance of the immobile trace elements in the mineral amendment.|5. The method of claim 1, wherein: the rare earth elements comprise scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), and lutetium (Lu); the rare metals comprise beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), titanium (Ti), vanadium (V), and zirconium (Zr); and the transition metals comprise nickel (Ni), chromium (Cr), and zinc (Zn).|6. The method of claim 1 wherein three immobile trace elements are measured.|7. The method of claim 6, wherein the three immobile trace elements are selected from the list comprising: (Y', 'La', 'Ce'), (Y', 'La', 'Pr'), (Y', 'La', Nd'), (Y', 'La', 'Sm'), (Y', 'La', 'Eh'), (Y', 'La', 'Gd'), (Y', 'La', 'Tb'), (Y', 'La', 'Dy'), (Y', 'La', 'Ho'), (Y', 'La', 'Er'), (Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), (Y', 'Ce', 'Pr'), (Y', 'Ce', 'Nd'), (Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eh'), (Y', 'Ce', 'Gd'), (Y', 'Ce', 'Tb'), (Y', 'Ce', 'Dy'), (Y', 'Ce', 'Ho'), (Y', 'Ce', 'Er'), (Y', 'Ce', 'Tm'), (Y', 'Ce', 'Yb'), (Y', 'Ce', 'Eh'), ('Y', 'Pr', 'Nd'), (Y', 'Pr', 'Sm'), (Y', 'Pr', 'Eu'), (Y', 'Pr', 'Gd'), (Y', 'Pr', 'Tb'), (Y', 'Pr', 'Dy'), (Y', 'Pr', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', Yb'), ('Y', 'Pr', 'Eh'), (Y', Nd', 'Sm'), (Y', d', 'Eh'), (Y', Nd', 'Gd'), (Y', Nd', 'Tb'), (Y', Nd', Dy'), (Y', Nd', 'Ho'), (Y', Nd', 'Er'), (Y', Nd', 'Tm'), (Y', Nd', Yb'), (Y', Nd', 'Lu'), (Y', 'Sm', 'Eu'), (Y', 'Sm', 'Gd'), (Y', 'Sm', 'Tb'), (Y', 'Sm', 'Dy'), (Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), (Y', 'Sm', 'Tm'), (Y', 'Sm', Yb'), (Y, 'Sm', 'Lu'), (Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), (Y', 'Eu', 'Dy'), (Y, 'Eu', 'Ho'), (Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), (Y', 'Eu', Yb'), ('Y', 'Eu', 'Lu'), (Y', 'Gd', 'Tb'), ('Y', Gd', 'Dy'), (Y', Gd', 'Ho'), (Y', 'Gd', 'Er'), (Y', 'Gd', 'Tm'), (Y, 'Gd', Yb'), (Y, 'Gd', 'Lu'), (Y', 'Tb', 'Dy'), (Y', 'Tb', 'Ho'), (Y', 'Tb', 'Er'), (Y', 'Tb', 'Tm'), (Y, 'Tb', Yb'), (Y', 'Tb', 'Lu'), (Y', 'Dy', 'Ho'), (Y', 'Dy', 'Er'), (Y, 'Dy', 'Tm'), (Y, 'Dy', Yb'), ('Y', Dy', 'Lu'), ('Y', 'Ho', 'Er'), (Y', 'Ho', 'Tm'), (Y', 'Ho', Yb'), (Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), (Y', 'Er', Yb'), (Y', 'Er', 'Lu'), (Y', 'Tm', Yb'), ('Y', 'Tm', 'Lu'), (Y', Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', Nd'), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', Dy'), ('La', 'Ce', 'Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', 'Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', Yb'), ('La', 'Pr', 'Lu'), ('La', Nd', 'Sm'), ('La', Nd', 'Eu'), ('La', Nd', 'Gd'), ('La', Nd', 'Tb'), ('La', Nd', 'Dy'), ('La', Nd', 'Ho'), ('La', Nd', 'Er'), ('La', Nd', 'Tm'), ('La', Nd', Yb'), ('La', Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), ('La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', Gd'), ('La', 'Eu', 'Tb'), ('La', 'Eu', Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'Gd', 'Tm'), ('La', Gd', Yb'), ('La', Gd', 'Lu'), ('La', 'Tb', 'Dy'), ('La', 'Tb', 'Ho'), ('La', 'Tb', 'Er'), ('La', 'Tb', 'Tm'), ('La', 'Tb', Yb'), ('La', 'Tb', 'Lu'), ('La', 'Dy', 'Ho'), ('La', 'Dy', 'Er'), ('La', 'Dy', 'Tm'), ('La', Dy', Yb'), ('La', Dy', 'Lu'), ('La', 'Ho', 'Er'), ('La', 'Ho', 'Tm'), ('La', 'Ho', Yb'), ('La', 'Ho', 'Lu'), ('La', 'Er', 'Tm'), ('La', 'Er', Yb'), ('La', 'Er', 'Lu'), ('La', 'Tm', Yb'), ('La', 'Tm', 'Lu'), ('La', Yb', 'Lu'), ('Ce', 'Pr', Nd'), ('Ce', 'Pr', 'Sm'), ('Ce', 'Pr', 'Eu'), ('Ce', 'Pr', 'Gd'), ('Ce', 'Pr', 'Tb'), ('Ce', 'Pr', 'Dy'), ('Ce', 'Pr', 'Ho'), ('Ce', 'Pr', 'Er'), ('Ce', 'Pr', 'Tm'), ('Ce', 'Pr', Yb'), ('Ce', 'Pr', 'Lu'), ('Ce', Nd', 'Sm'), ('Ce', Nd', 'Eu'), ('Ce', Nd', Gd'), ('Ce', Nd', 'Tb'), ('Ce', Nd', 'Dy'), ('Ce', Nd', 'Ho'), ('Ce', Nd', 'Er'), ('Ce', Nd', 'Tm'), ('Ce', Nd', Yb'), ('Ce', Nd', 'Lu'), ('Ce', 'Sm', 'Eu'), ('Ce', 'Sm', 'Gd'), ('Ce', 'Sm', 'Tb'), ('Ce', 'Sm', 'Dy'), ('Ce', 'Sm', 'Ho'), ('Ce', 'Sm', 'Er'), ('Ce', 'Sm', Tm'), ('Ce', 'Sm', 'Yb'), ('Ce', 'Sm', 'Lu'), ('Ce', 'Eu', 'Gd'), ('Ce', 'Eii', Tb'), ('Ce', 'Eu', 'Dy'), ('Ce', 'Eu', 'Ho'), ('Ce', 'Eu', 'Er'), ('Ce', 'Eu', 'Tm'), ('Ce', 'Eu', Yb'), ('Ce', 'Eu', 'Lu'), ('Ce', 'Gd', 'Tb'), ('Ce', 'Gd', 'Dy'), ('Ce', Gd', 'Ho'), ('Ce', 'Gd', 'Er'), ('Ce', 'Gd', 'Tm'), ('Ce', 'Gd', Yb'), ('Ce', 'Gd', 'Lu'), ('Ce', 'Tb', 'Dy'), ('Ce', 'Tb', 'Ho'), ('Ce', 'Tb', 'Er'), ('Ce', 'Tb', 'Tm'), ('Ce', 'Tb', Yb'), ('Ce', 'Tb', 'Lu'), ('Ce', 'Dy', 'Ho'), ('Ce', Dy', 'Er'), ('Ce', 'Dy', 'Tm'), ('Ce', 'Dy', Yb'), ('Ce', 'Dy', 'Lu'), ('Ce', 'Ho', 'Er'), ('Ce', 'Ho', 'Tm'), ('Ce', 'Ho', Yb'), ('Ce', 'Ho', 'Lu'), ('Ce', 'Er', 'Tm'), ('Ce', 'Er', Yb'), ('Ce', 'Er', 'Lu'), ('Ce', 'Tm', Yb'), ('Ce', 'Tm', 'Lu'), ('Ce', Yb', 'Lu'), ('Pr', 'Nd', 'Sm'), ('Pr', 'Nd', 'Eu'), ('Pr', 'Nd', Gd'), ('Pr', 'Nd', 'Tb'), ('Pr', 'Nd', Dy'), ('Pr', 'Nd', 'Ho'), ('Pr', Yd', 'Er'), ('Pr', Yd', 'Tm'), ('Pr', Yd', Yb'), ('Pr', Yd', 'Lu'), ('Pr', 'Sm', 'Eu'), ('Pr', 'Sm', 'Gd'), ('Pr', 'Sm', 'Tb'), ('Pr', 'Sm', Dy'), ('Pr', 'Sm', 'Ho'), ('Pr', 'Sm', 'Er'), ('Pr', 'Sm', 'Tm'), ('Pr', 'Sm', Yb'), ('Pr', 'Sm', 'Lu'), ('Pr', 'Eu', Gd'), ('Pr', 'Eu', 'Tb'), ('Pr', 'Eu', 'Dy'), ('Pr', 'Eu', 'Ho'), ('Pr', 'Eu', 'Er'), ('Pr', 'Eu', 'Tm'), ('Pr', 'Eu', Yb'), ('Pr', 'Eu', 'Lu'), ('Pr', Gd', 'Tb'), ('Pr', 'Gd', Dy'), ('Pr', 'Gd', 'Ho'), ('Pr', 'Gd', 'Er'), ('Pr', 'Gd', 'Tm'), ('Pr', 'Gd', Yb'), ('Pr', 'Gd', 'Lu'), ('Pr', 'Tb', 'Dy'), ('Pr', 'Tb', 'Ho'), ('Pr', 'Tb', 'Er'), ('Pr', 'Tb', 'Tm'), ('Pr', 'Tb', Yb'), ('Pr', 'Tb', 'Lu'), ('Pr', 'Dy', 'Ho'), ('Pr', 'Dy', 'Er'), ('Pr', Dy', 'Tm'), ('Pr', Dy', Yb'), ('Pr', 'Dy', 'Lu'), ('Pr', 'Ho', 'Er'), ('Pr', 'Ho', 'Tm'), ('Pr', 'Ho', Yb'), ('Pr', 'Ho', 'Lu'), ('Pr', 'Er', 'Tm'), ('Pr', 'Er', Yb'), ('Pr', 'Er', 'Lu'), ('Pr', 'Tm', Yb'), ('Pr', 'Tm', 'Lu'), ('Pr', Yb', 'Lu'), (Yd', 'Sm', 'Eu'), (Yd', 'Sm', 'Gd'), (Yd', 'Sm', 'Tb'), (Yd', 'Sm', 'Dy'), (Yd', 'Sm', 'Ho'), (Yd', 'Sm', 'Er'), (Yd', 'Sm', 'Tm'), (Yd', 'Sm', Yb'), (Yd', 'Sm', 'Lu'), (Yd', 'Eu', 'Gd'), (Yd', 'Eu', 'Tb'), (Yd', 'Eu', 'Dy'), (Yd', 'Eu', 'Ho'), (Yd', 'Eu', 'Er'), (Yd', 'Eu', 'Tm'), (Yd', 'Eu', Yb'), (Yd', 'Eu', 'Lu'), (Yd', 'Gd', 'Tb'), (Yd', 'Gd', 'Dy'), (Yd', Gd', 'Ho'), (Yd', 'Gd', 'Er'), (Yd', 'Gd', 'Tm'), (Yd', 'Gd', Yb'), (Yd', 'Gd', 'Lu'), (Yd', 'Tb', Dy'), (Yd', 'Tb', 'Ho'), (Yd', 'Tb', 'Er'), (Yd', 'Tb', 'Tm'), (Yd', 'Tb', Yb'), (Yd', 'Tb', 'Lu'), (Yd', 'Dy', 'Ho'), (Yd', 'Dy', 'Er'), (Yd', 'Dy', 'Tm'), (Yd', 'Dy', Yb'), (Yd', 'Dy', 'Lu'), (Yd', 'Ho', 'Er'), (Yd', 'Ho', 'Tm'), (Yd', 'Ho', Yb'), (Yd', 'Ho', 'Lu'), (Yd', 'Er', 'Tm'), (Yd', 'Er', Yb'), (Yd', 'Er', 'Lu'), (Yd', 'Tm', Yb'), (Yd', 'Tm', 'Lu'), (Yd', Yb', 'Lu'), ('Sm', 'Eu', 'Gd'), ('Sm', 'Eu', 'Tb'), ('Sm', 'Eu', 'Dy'), ('Sm', 'Eu', 'Ho'), ('Sm', 'Eu', 'Er'), ('Sm', 'Eu', 'Tm'), ('Sm', 'Eu', Yb'), ('Sm', 'Eu', 'Lu'), ('Sm', 'Gd', 'Tb'), ('Sm', 'Gd', 'Dy'), ('Sm', 'Gd', 'Ho'), ('Sm', 'Gd', 'Er'), ('Sm', 'Gd', 'Tm'), ('Sm', 'Gd', Yb'), ('Sm', 'Gd', 'Lu'), ('Sm', 'Tb', 'Dy'), ('Sm', 'Tb', 'Ho'), ('Sm', 'Tb', 'Er'), ('Sm', 'Tb', 'Tm'), ('Sm', 'Tb', Yb'), ('Sm', 'Tb', 'Lu'), ('Sm', Dy', 'Ho'), ('Sm', 'Dy', 'Er'), ('Sm', Dy', 'Tm'), ('Sm', 'Dy', Yb'), ('Sm', Dy', 'Lu'), ('Sm', 'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', Yb'), ('Sm', 'Ho', 'Lu'), ('Sm', 'Er', 'Tm'), ('Sm', 'Er', Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', Yb', 'Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', 'Gd', Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('Eu', 'Tb', Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', Dy', 'Tm'), ('Eu', Dy', Yb'), ('Eu', Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'Tm'), ('Eu', 'Er', Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', Yb', 'Lu'), ('Gd', 'Tb', Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', Dy', Yb'), ('GcT, 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', Tm1), (Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), (Gd', 'Er', Tm'), ('Gd', 'Er', Yb'), ('Gd', 'Er', 'Lu'), ('Gd', 'Tm', Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', 'Dy', 'Tm'), ('Tb', Dy', Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', Yb'), ('Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', Yb'), ('Tb', 'Tm', 'Lu'), ('Tb', Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', Yb', 'Lu'), (Ho', 'Er', 'Tm'), (Ho', 'Er', Yb'), (Ho', 'Er', 'Lu'), (Ho', 'Tm', Yb'), (Ho', 'Tm', 'Lu'), (Ho', Yb', 'Lu'), ('Er', 'Tm', Yb'), ('Er', 'Tm', 'Lu'), ('Er', Yb', 'Lu'), and ('Tm', Yb', 'Lu').|8. The method of claim 1, wherein the step of measuring the immobile trace elements in a soil sample after application of the mineral amendment further comprises lysing the soil sample and application of ethylenediaminetetraacetic acid. (EP4256520)|Cross Reference to Related Applications|[0001] The present applications claims the priority benefit of U.S. Provisional Patent App. Serial No. 63/322,672, filed March 23, 2022; U.S. Provisional Patent App. Serial No. 63/289,395, filed December 14, 2021; and U.S. Provisional Patent App. Serial No. 63/213,398, filed, June 22, 2021.|Background|[0002] The last several years have witnessed a maturation of carbon markets from lightly scrutinized voluntary markets largely serving to provide positive marketing collateral to familiar consumer brands to rigorous compliance markets with proof-of-performance requirements often involving government and quasi-governmental regulators. There have also been a number of comprehensive proposals for decarbonization of the entire US economy, combining energy production, transportation, cement production, and agriculture. These proposals have included carbon dioxide removal (CDR) techniques as an essential component of the decarbonization plan, with a supportive ecosystem of science, policy, and project evaluation criteria. Within the diverse scope of decarbonization efforts, including renewable energy, biofuel, nature-based solutions, and more technical CDR techniques like direct air capture (DAC), The Oxford Principles have developed a taxonomy for categorizing diverse decarbonization strategies. This taxonomy distinguishes between avoided emissions (for instance, conversion of fossil fuel power to renewable power) and negative emissions (for instance direct air capture); distinguishes between avoided emissions that require storage (for instance carbon capture from a point source and sequestration into the ground) and those that do not require storage (the conversion to renewable energy); and the duration of the storage if so required (for instance, short lived forest carbon sequestration from delayed harvests versus storage of captured carbon in geological formations).|[0003] A number of for-profit and non-profit organizations have emerged that employ the Oxford Principles to evaluate proposals, particularly around the rigorous quantification across categories (Table 1). This, in essence, is the scorecard that projects will have to compete on to find acceptance in the industry. All other things equal, cost ends up being the primary driver, but quality is also a key consideration. Thus, historically buyers have been drawn to nature-based solutions that cost between $5-20/tCO2 e (e.g., Corteva Carbon, Indigo Carbon), versus direct air capture projects that cost >$500/tCO2 e (e.g., ClimeWorks). However, there are challenges to these nature-based solutions: recently these nature-based solutions have been subject to intense scrutiny for "gaming" the rules or otherwise failing to deliver prospective rewards. Among the technological solutions, there are a different set of challenges: rigor has been strong, but the reduction in price proportional to increase in deployment has been slow, and the ultimate price of DAC is not expected to drop below $150/tCO2e (Keith et al 2018, https://doi.org/10.1016/j.joule.2018.05.006). In light of these challenges, we have developed a technology around "enhanced rock weathering" (ERW), in which silicate minerals are weathered in acidic soil solution, thus driving the uptake of additional CO2 into dissolved inorganic carbon (DIC) in the soil solution. Our experimental work, life cycle analysis, and techno-economic modeling have indicated that ERW provides the permanence, additionality, and rigorous quantification of a DAC project, the large volume of a carbon capture and storage (CCS) project, and the unit economics of a nature based solution, thus creating a new tool to meet net-zero goals.|Details of Enhanced Rock Weathering|[0004] In "enhanced rock weathering" (ERW), silicate minerals are weathered by CO2 from the ambient air which has been dissolved into water, reacting to produce dissolved inorganic carbon that is ultimately stored in the ocean as depicted in FIGS. 1 and 2.|Background Geochemistry|[0005] The role of silicate rock weathering in maintaining the CO2 balance of the atmosphere has been recognized for decades, first outlined by renowned chemist Harold Urey in the 1950s. The basic premise of the Urey reaction is that continental collisions release CO2 to the atmosphere from volcanoes, and bring Mg- and Ca-bearing silicate rocks to the surface. The rainwater (H2O) that falls upon these rocks is mildly acidic, as atmospheric CO2 has dissolved in it and formed carbonic acid (H2CO3). For forsterite, the weathering reaction takes place following the form:|        Mg2SiO4 + 4 H2O + 4 CO2 → 2 Mg2+ + 4 HCO3- + 4 H4SiO4|[0006] In this reaction, one mole of forsterite consumes four moles of CO2, so two negatively charged bicarbonate HCO3- are created for every one divalent Mg2+ weathered. Given the molecular weight of forsterite (140 g/mol) and the molecular weight of CO2 (44 g/mol), weathering one metric ton of forsterite removes 1.25 metric tons of CO2 from the atmosphere. In general, such a formula can be used to define the "mineral potential" of a silicate based on its elemental composition: | where V is the valence of the cation (2 for Mg and Ca) and MW is the molecular weight.|[0007] The rate of weathering is determined by the surface area of the mineral, the acidity (pH) of the soil solution, the temperature of the solution, the availability of CO2 reagent in solution, and the rate of removal of the reaction products by water. One of the key insights into the potential of "enhanced" rock weathering is that the rate of reaction, and thus CO2 removal, can be greatly accelerated by increasing the surface area by pulverization into a fine powder (e.g., less than 100 um), incorporating into an acidic environment (e.g., pH less than 6) with abundant CO2 present, and with steady water flux to remove reaction products to maintain acidity. While this formula defines the potential amount of CO2 that may be removed by weathering, it does not speak to the rate; ancient rock formations testify that the rate of weathering can be extremely slow.|[0008] The relationship between silicates (like Mg2SiO4) and dissolved carbonates (like HCO3-) is not necessarily intuitive, as the carbonate system of water involves a number of coupled reactions. Atmospheric CO2 dissolves into water according to an exchange coefficient:|        CO2(aq) = H2CO3 = KCO2 * pCO2|[0009] Technically pCO2 is "fugacity" that represents its activity, but, as used herein, it is more or less equivalent to its partial pressure, and KCO2 is the Henry's law coefficient that determines the aqueous CO2 in equilibrium with the atmosphere. This aqueous CO2 in turn hydrates with H2O to become carbonic acid (H2CO3), which dissociates to become bicarbonate (HCO3-) and carbonate (CO32-):|        H2CO3 ↔ HCO3- + H+|        HCO3- ↔ CO32- + H+|[0010] These equilibrium reactions are defined by K1 and K2, the first and second carbonate system dissociation constants. pK1 and pK2 are about 5.9 and about 9.4 at STP, so greater than 99% of the charge in the dissolved carbonates is HCO3-.|[0011] The carbonates are the largest constituents of total alkalinity, which is defined as the charge imbalance between weak acids (proton acceptors) minus proton donors:|        TA = [HCO3-] + 2 · [CO32-] + [OH-] - [H+]|[0012] There is an alternative definition of total alkalinity as the charge imbalance between conserved cations and conserved anions:|        TA = [Na+] + 2 [Mg2+] + 2 [Ca2+] + [K+] + ... - [Cl-] - 2 [SO42-] - [NO3-]|[0013] These two expressions are always equal (i.e. the charges balance). This means that an added Mg or Ca into soil solution will increase in HCO3- to balance the charge. We describe an analytical solution to compute how much carbon is taken up per unit of additional Mg or Ca. If we first define DIC as the sum of H2CO3, HCO3-, and CO32-, and make use of the equilibrium equations above (defining H+ as "h" and H2CO3 as "s"): |[0014] And formulate TA using the same convention: |[0015] With these definitions in place, we can develop an estimate of dDIC/dTA. First, we compute the derivative dTA/dh: |[0016] Next we compute the derivative dDIC/dh: |[0017] Finally we multiply dDIC/dh by the inverse of dTA/dh to calculate dDIC/dTA: |[0018] At the pH found in soils, each Mg or Ca is matched by two carbon atoms. In all circumstances, raising alkalinity results in increased pH. This is particularly important in marine settings, where ocean acidification from increased atmospheric CO2 can be ameliorated by this export of alkalinity from land.|[0019] The potential for ERW as a commercial enterprise is limited by some fundamental issues:| A. The total amounts of mineral transformation and carbon removal should be verifiable empirically. The verification methods described below may be low cost at scale, can be performed at arm's length by a 3rd party, and may have safeguards to eliminate fraud.|[0020] Additionally, the commercial potential for ERW could be enhanced by a number of different features. Embodiments may include:| B. Processes and modifications of the engineered mineral product that enhance the agronomic performance and ecosystem co-benefits of the engineered mineral.| C. Processes and modifications of the engineered mineral product that control or enhance the mineral dissolution rate of the engineered mineral in soil environments and thus the rate of removal of CO2.| C. Paulo et al, Applied Geochemistry, 2021, 219, 104955, discusses evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralisation.| N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809 discusses carbon dioxide efficiency of terrestrial enhanced weathering and determination of effective carbon dioxide sequestration.|Brief Description of the Drawings|[0021] FIG. 1 is a drawing illustrating the enhanced rock weathering cycle.| FIG. 2 is a graph depicting the effect of comminution on dissolution kinetics for a silicate.| FIGS. 3A to 3D are graphs depicting the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um which closely approximates the alkalinity release dynamics for aglime.| FIG. 4 is a drawing illustrating the general scheme for a verified enhanced rock weathering cycle.|Detailed Description|[0022] Summary: The following described methodologies can establish one version of a verification scheme that will demonstrate the transformation of the applied rock material and the subsequent carbon removal into secure geologic reservoirs as evidenced by observations collected from the soil. One set of methods (A) can measure the production of free ions from the applied material and the transport of those ions outside of a control volume as a direct measure of the amount of weathering and thus total carbon dioxide equivalent isolated from the atmosphere. Furthermore, as the elemental inputs into the soil induced by enhanced rock weathering can have significant effects on the soil geochemistry, methods in (B) describe systems and versions that can enhance the agronomic performance of the soil amendment and increase ecosystem co-benefits. Lastly, methods in (C) elaborate on versions that control and enhance the mineral dissolution rate, which increases the financial performance of enhanced rock weathering technology in the marketplace.| A. Systems and methods for monitoring and verification:Described below are several example methodologies for quantifying the rate and extent of mineral transformation and carbon removal, which are referred to as "verification methodologies".1. Example Verification methodology 1:a. A cation exchange resin and/or an anion exchange resin are packaged into a physical embodiment (such as a 5 cm diameter tube, 5cm in length, placed 30 cm below the soil surface) that allows vertical transport of fluids but not horizontal transport.| b. Commercial ion exchange resins are pre-equilibrated in such a way that their selectivity is high for the relevant ions, but their capacity is also sufficiently high such that saturation is minimized. This technology may allow for effective deployment for long periods of time, allowing passage of up to 4000 mm of moisture through the tube, without becoming saturated with respect to the ions of interest.| c. The ions of interest are restricted to divalent cations (Mg2+, Ca2+), carbonate species (HCO3- and CO32-), and silicic acid (H4SiO4), important weathering products of preferred mineral soil amendments, such as ultramafic rocks, blast furnace slag, and other naturally occurring or industrial silicate minerals with high Mg and Ca content.| d. Three pre-equilibrated tubes are emplaced fully under the soil below a control depth (e.g., 30 cm, a typical depth of cultivation). This may be done by removing the top 30 cm soil with a shovel or auger, then gently placing the tube in the created void space. Following a certain period of time post-surface application of mineral soil amendment (e.g., 9 to 12 months after application), the tubes are retrieved, and the ions captured within the resin exchanges are measured using standard methodologies, such as ICP-OES and ICP-MS based concentration measurements. Three tubes are used to determine standard deviation error in triplicate.| e. By the principle of charge balance and known thermodynamic reactions taking place in the top 30 cm of soils, the amount of carbonate can be inferred purely from the measurement of cations, under certain assumptions and auxiliary geochemical data. By the addition of more specific anion exchange resins, such as styrenedivinylbenzene, these assumptions can be avoided to get a more precise answer. The increase in cation concentration in the subsurface soil pore water allows for the stoichiometric determination of carbon removal from the gas phase (ambient air).| f. The total carbon dioxide removed during the deployment period may be estimated as equal to the molecular mass of CO2 (44 g/mol) multiplied by the sum of the number of moles of carbonate and two times the number of moles of bicarbonate, multiplied by the area on which mineral was applied to the field, divided by the cross-sectional area of the tube.| g. Direct measurement of aqueous bicarbonate and carbonate species, which are the most readily available forms of carbon induced by a gas exchange of carbon dioxide with the soil pore water, may be conducted using the specified anion exchange resin above. The expression as described in clause (f) explains the calculation used to convert this direct measurement of carbon to an absolute value of carbon dioxide removed during a specified application period.| h. Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.| i. However, potential disadvantages may include the need for manufacturing (and its attendant demand for working capital); devices may occasionally be defective; emplacement of a device may alter the flow paths of water, which in turn alters the inferred ion fluxes; emplacement of a device may depend on the user; the knowledge of the location of emplacement may invite manipulation by a stakeholder involved in a carbon transaction; and others. 2. Example Verification methodology 2:a. The principle behind Verification methodology 2 is that minerals applied for purposes of enhanced rock weathering contain, in addition to the elements outlined above that participate in the weathering reaction (i.e., magnesium, calcium, iron, silicon, oxygen, hydrogen), additional elements in trace amounts. These additional trace elements (TEs) might include rare earth elements (REEs), rare metals (RM), other transition metals (TMs), or a combination thereof. Unlike the primary weathering products that are readily dissolved in solution and lost by leaching, some TEs are strongly bound to mineral and biological surfaces and do not readily leach from the soil control volume (e.g., the top 10 to 30 cm of soil), and are not removed by plants at the concentrations present in our applied rock. These strongly bound trace elements are referred to herein as immobile trace elements (ITEs). Thus, a measure of cumulative cation flux and carbon removal can be computed by comparing the ratio of the lost weathering products, such as magnesium, to ITEs, after accounting for background concentrations of ITEs in the initial soil.| b. As used herein, rare earth elements include scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), lutetium (Lu) or a combination thereof. As used herein, rare metals include beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), zirconium (Zr), or a combination thereof. As used herein, transition metals include nickel (Ni), chromium (Cr), and zinc (Zn) among others and may include a combination of transition metals.| c. An approach based on ITEs depends on the degree of immobility of the element in soil environments, the time horizon after which the ITEs will be measured to estimate carbon removal, the abundance of ITEs in both the soil and the mineral added, and the analytical chemistry used to measure this abundance. An analytical technique that has low detectability thresholds for slightly mobile elements could be sufficient for relatively abundant (e.g., parts per thousand to parts per million) elements over short time horizons (e.g., weeks to months). On the other hand, a different analytical technique could be used over longer time horizons, which in turn could involve quantification of very immobile elements that are present in much lower abundance (e.g., parts per billion to parts per trillion). The approach may be chosen based at least in part on cost, which ITEs are actually conserved, over which time horizons, as well as the performance of the analytical performance used.| d. The relative proportions of ITEs in a sample (rock or soil) constitute a type of unique fingerprint of the material. Because the cost of pure ITEs is large, and the analytical chemistry is not widely available, there is a significant barrier to engineering a fraudulent sample to reproduce the native ITE fingerprint of a mineral soil amendment. Thus, it would be challenging for a stakeholder in a carbon exchange transaction to generate a result that produces the anticipated result (a high or low amount of carbon removal) while also matching the ITE fingerprint generated by a bona fide sample. This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).| e. Verification Methodology 2 (VM2) has advantages over Verification Methodology 1 (VM1) in that it avoids the need for the use of a device, which avoids altering the soil hydrology or physical environment in a way that would impact the observed elemental analysis.| f. VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.| g. VM2 does, however, include measurement techniques that are less widely available; requires specialized instruments and personnel; requires additional boundary conditions to compute carbon flux (e.g., pre-application soil and rock elemental analysis); and employs assumptions as to the relationship between cation flux and carbon flux.| h. Like VM1, VM2 uses the total amount of mineral applied and the field area, which could be measured, for example, using a digital as-applied map commonly accompanying crops input machinery, or truck weights before and after mineral delivery. This will be referred to as the nominal application rate (ARnominal).| i. There are four main calculations in VM2. To the extent any one of these factors is known unambiguously from other sources, each step in VM2 could be used in isolation from the others.i. Classify, using ITE fingerprinting, whether a soil has had a specific mineral applied, which may be asserted by an entity wishing to make a claim;| ii. Calculate, using ITE fingerprinting, what the actual mineral application rate (ARactual) for a specific soil sample was, which will necessarily differ in a systematic or random way from the average rate for the entire field;| iii. Calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the application rate in (ii) above;| iv. Calculate, using the fraction computed in (iii) and the mineral potential (Equation 1) computed for the feedstock identified in (i) above, the amount of carbon dioxide removed. j. In one non-limiting embodiment, the verification methodology to classify whether the claimed mineral applied is the actual mineral applied is as follows:i. Collect a sample from mineral to be applied, place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Mineral Amendment.| ii. Prior to mineral application, collect a 20 g sample from cultivated zone of soil (typically at around 30 cm, such as in a range of 0 cm to 30 cm), place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Soil A.| iii. Subsequent to mineral application, collect a 20 g sample the same control zone as soil A, and store under similar conditions. Label as Soil B. Soil B could be sampled immediately after mineral application or at a later time (e.g., months to years afterwards).| iv. Characterize the elemental composition of Mineral Amendment, Soil A, and Soil B. Example approaches to characterizing the elemental composition are described in (v) and (vi).| v. One approach to measuring the elemental composition is as follows:1. In a laboratory setting, unseal the soil samples and place 10 grams of Soil A and Soil B in two separate beakers.| 2. Dissolve the solids in strong acid. For example, add 21 mL of strong 1.0 M hydrochloric acid and 7 mL of strong 1.0 M nitric acid (total 28 mL acid) to each beaker of sterilized soil and stir rigorously until solids are dissolved.| 3. Filter the sample-containing beakers first through a 1- to 5-micron water filter cartridge followed by an attached 10 to 20 cm column cation exchange resin at a sufficiently slow flow rate of, for example, 1 to 5 mL/min. This combination of a water filter with a cation exchange column has been engineered for optimal performance with soils under consideration. Specifically, the 5-micron water filter cartridge separates out any larger particles, allowing for the smaller particles to exchange its bound metals with the subsequent cation exchange resin.| 4. Flush copious amounts (e.g., 100-200 mL) of 0.5 to 1.0 M chelator such as, for example, ethylenediaminetetraacetic acid (EDTA) at 1-5 mL/min through the used filters into their respective filtrates. This may collect any additional metals that were still adhered to the filters.| 5. Send filtrate A (resultant sample from Soil A) and filtrate B (resultant sample from Soil B) to an analytical laboratory for analysis on an inductively coupled plasma mass spectrometer (ICP-MS). Measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3.| 6. The ICP-MS may be set to detect magnesium concentrations and the following 17 elements on a high ppb or low ppm detection level: Yttrium, Scandium, Lanthanum, Cerium, Praseodymium, Neodymium, Promethium, Samarium, Europium, Gadolinium, Terbium, Dysprosium, Holmium, Erbium, Thulium, Ytterbium, Lutetium. Classify light rare earth elements (LREEs) as yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium. Classify heavy rare earth elements (HREEs) as europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium. Send an isolated rock material sample for ICP-MS analysis. Similar to the filtrate analyses, measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3. vi. Another approach to measuring the elemental composition is as follows:1. Calibrate a portable XRF instrument for particularly low detection limit of ITEs using a calibration standard (such as Bruker proprietary Geo calibration + custom ITE standards).| 2. Use the portable XRF instrument to analyze the Rock Material and Soil A for ITEs (as identified in Verification methodology 2), reporting the instrumental error (2 standard deviations) as well.| 3. Use the portable XRF instrument to analyze Soil B for ITEs, reporting the instrumental error (2 standard deviations) as well. vii. Once the above elemental composition has been determined, calculate the difference for every element between Mineral Amendment and Soil A, resulting in a vector of differences vrock. Likewise, compute the difference for every element between Soil B and Soil A, resulting in a vector of differences vsoil. To improve performance, each element may be divided by an individual factor, such as the detection threshold, or the instrumental uncertainty, or the elemental composition of a reference material. Another means to improve performance would be to sum a subset of the elements or several distinct subsets of elements before computing vrock and vsoil. Another means to improve performance would be to compute indices of these summed subsets of elements, for example the ratio of the light REEs to the heavy REEs, before computing vrock and vsoil.| viii. Compute the dot product of vrock and vsoil. If the value of this dot product is close to 1 (e.g., within a threshold value), then the Soil B is positively classified as having the Mineral Amendment. If the value of the dot product is less than 1 minus a threshold value, then Soil B is negatively classified as not having the Mineral Amendment.| ix. The threshold value may be determined using a variety of means, for example the half-angle between the dot product of vrock and vsoil and any other known vrock and vsoil; or using a Monte Carlo simulation of vrock and vsoil that accounts for known sources of uncertainty including instrumental error, variation in rock elemental analysis, or variation of soil elemental analysis. k. In one non-limiting embodiment, the verification methodology to calculate the actual mineral application rate (ARactual) for a specific soil sample is as follows:i. Characterize the elemental composition the elemental composition of Mineral Amendment, Soil A, and Soil B as above. Note that there could be different analytical chemistry employed if, for example, rapid and inexpensive XRF analysis was used for classification soon after application, and slower and more costly ICP analysis may be used to estimate application rates.| ii. Compute the differences in elemental composition as above, potentially including similar performance enhancements such as normalizing by factors specific to each element, summing across subsets of elements, and computing indices such as the ratio of light REEs to heavy REEs. Such transformed and summed variables for a sample will be referred to generically as ΣITEsample.| iii. The actual application rate of the sample can be calculated using the following expression: l. In one non-limiting embodiment, the verification methodology to calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the actual mineral application rate (ARactual) as follows:i. The amount of divalent cations applied (DCapplied) can be calculated by the proven identity of the mineral additive and the actual application rate: where divalent cations are generally restricted in this context to Mg and Ca, and Mgmineral and Camineral is the fractional composition of the mineral additive.| ii. The amount of divalent cations remaining (DCremain) in the soil could be estimated using the same elemental analysis as previously (if, for example, ICP-MS was used), or determined from the same sample using a different analysis (if, for example XRF was used and Mg was not measured).| iii. The fractional progress of carbon dioxide removal (CDR) can be estimated by the ratio of remaining divalent cations to applied divalent cations: m. In one non-limiting embodiment, the verification methodology to calculate the amount of carbon dioxide removed from the control volume is as follows:i. Assembling MP, fCDR , ARnominal and the land area applied, the total carbon dioxide removal is: n. While Verification Methodology 2 presented herein provides a broad framework for the detection and application of soil-bound ITEs to estimate long-term geologic carbon drawdown, the efficacy of the approach can also be improved through the focus on specific subsets of ITEs. Non-limiting embodiments of such improvements are listed below:i. The ITEs specified in equation 2, e.g., (ΣITEssoil B), may in fact be represented not by the full summation of 17 REEs but instead by the use of only LREEs or the use of only HREEs, as defined in clause xii. Such a calculation would mean the sum of only LREEs in the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium) or the sum of only HREEs in the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium).| ii. Within the use of only LREEs for the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium), some LREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual LREEs are selected. For example, the subset may include three LREEs. The calculation (equation 2) is conducted for each of the 3 LREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 LREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [yttrium, scandium, lanthanum], [cerium, lanthanum, neodymium], [cerium, neodymium, samarium], [yttrium, cerium, neodymium], [scandium, neodymium, samarium].| iii. Within the use of only HREEs for the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium), some HREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual HREEs are selected. For example, the subset may include three HREEs. The calculation (equation 2a) is conducted for each of the 3 HREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 HREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [europium, gadolinium, terbium], [europium, terbium, dysprosium], [dysprosium, erbium, ytterbium], [europium, erbium, ytterbium], [europium, dysprosium, erbium].| iv. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual REEs are selected. For example, the subset may include three REEs Chart 1 represents a non-limiting list of REE triplicates that may enhance the efficacy of this C drawdown calculation.Chart 1. A non-limiting list of 455 REE triplicates that can be used to effectively triangulate a C drawdown estimation|('Y', 'La', 'Ce'), ('Y', 'La', 'Pr'), ('Y', 'La', 'Nd'), ('Y', 'La', 'Sm'), ('Y', 'La', 'Eu'), ('Y', 'La', 'Gd'), ('Y', 'La', 'Tb'), ('Y', 'La', 'Dy'), ('Y', 'La', 'Ho'), ('Y', 'La', 'Er'), ('Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), ('Y', 'Ce', 'Pr'), ('Y', 'Ce', 'Nd'), ('Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eu'), ('Y', 'Ce', 'Gd'), ('Y', 'Ce', 'Tb' ), ('Y', 'Ce', 'Dy'), ('Y', 'Ce', 'Ho'), ('Y', 'Ce', 'Er'), ('Y', 'Ce', 'Tm'), ('Y', 'Ce', 'Yb'), ('Y', 'Ce', 'Lu'), (' Y', 'Pr', 'Nd'), ('Y', 'Pr', 'Sm'), ('Y', 'Pr', 'Eu'), ('Y', 'Pr', 'Gd'), ('Y', 'Pr', 'Tb'), ('Y', 'Pr', 'Dy'), ('Y', 'Pr ', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', 'Yb'), ('Y', 'Pr', 'Lu'), ('Y', 'Nd', 'Sm'), ('Y', 'Nd', 'E u'), ('Y', 'Nd', 'Gd'), ('Y', 'Nd', 'Tb'), ('Y', 'Nd', 'Dy'), ('Y', 'Nd', 'Ho'), ('Y', 'Nd', 'Er'), ('Y', 'Nd', 'Tm' ), ('Y', 'Nd', 'Yb'), ('Y', 'Nd', 'Lu'), ('Y', 'Sm', 'Eu'), ('Y', 'Sm', 'Gd'), ('Y', 'Sm', 'Tb'), ('Y', 'Sm', 'Dy'), ('Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), ('Y', 'Sm', 'Tm'), ('Y', 'Sm', 'Yb'), ('Y', 'Sm', 'Lu'), ('Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), ('Y', 'Eu', 'Dy'), ('Y', 'Eu', 'Ho'), ('Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), ('Y', 'Eu', 'Yb'), ('Y ', 'Eu', 'Lu'), ('Y', 'Gd', 'Tb'), ('Y', 'Gd', 'Dy'), ('Y', 'Gd', 'Ho'), ('Y', 'Gd', 'Er'), ('Y', 'Gd', 'Tm'), ('Y', ' Gd', 'Yb'), ('Y', 'Gd', 'Lu'), ('Y', 'Tb', 'Dy'), ('Y', 'Tb', 'Ho'), ('Y', 'Tb', 'Er'), ('Y', 'Tb', 'Tm'), ('Y', 'Tb ', 'Yb'), ('Y', 'Tb', 'Lu'), ('Y', 'Dy', 'Ho'), ('Y', 'Dy', 'Er'), ('Y', 'Dy', 'Tm'), ('Y', 'Dy', 'Yb'), ('Y', 'Dy', 'Lu'), ('Y', 'Ho', 'Er'), ('Y', 'Ho', 'Tm'), ('Y', 'Ho', 'Yb'), ('Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), ('Y', 'Er', 'Y b'), ('Y', 'Er', 'Lu'), ('Y', 'Tm', 'Yb'), ('Y', 'Tm', 'Lu'), ('Y', 'Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', 'Nd' ), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', 'Dy'), ('La', 'Ce', ' Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', 'Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', 'Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', 'Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', ' Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', 'Yb'), ('La', 'Pr', 'Lu'), ('La', 'Nd', 'Sm'), ('La', 'Nd', 'Eu'), ('La', 'Nd', 'Gd'), ('La', 'Nd', 'Tb'), ('La', 'Nd', 'Dy'), ('La', 'Nd', 'Ho'), ('La', 'Nd', 'Er'), ('La', 'Nd', 'Tm'), ('La', ' Nd', 'Yb'), ('La', 'Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), (' La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', 'Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', 'G d'), ('La', 'Eu', 'Tb'), ('La', 'Eu', 'Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', ' Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'G d', 'Tm'), ('La', 'Gd', 'Yb'), ('La', 'Gd', 'Lu'), ('La', 'Tb', 'Dy'), ('La', 'Tb', 'Ho'), ('La', 'Tb', 'Er'), ('La', 'Tb', 'Tm'), ('La', 'Tb', 'Yb'), ('La', 'Tb', 'Lu'), ('La', 'Dy', 'Ho'), ('La', 'Dy', 'Er'), ('La', 'Dy', 'Tm'), ('L a', 'Dy', 'Yb'), ('La', 'Dy', 'Lu'), ('La', 'Ho', 'Er'), ('La', 'Ho', 'Tm'), ('La', 'Ho', 'Yb'), ('La', 'Ho', 'Lu'), ('La', 'Er', 'Tm'), ('La', 'Er', 'Yb'), ('La', 'Er', 'Lu'), ('La', 'Tm', 'Yb'), ('La', 'Tm', 'Lu'), ('La', 'Yb', 'Lu' ), ('Ce', 'Pr', 'Nd'), ('Ce', 'Pr', 'Sm'), ('Ce', 'Pr', 'Eu'), ('Ce', 'Pr', 'Gd'), ('Ce', 'Pr', 'Tb'), ('Ce', 'Pr', 'Dy' ), ('Ce', 'Pr', 'Ho'), ('Ce', 'Pr', 'Er'), ('Ce', 'Pr', 'Tm'), ('Ce', 'Pr', 'Yb'), ('Ce', 'Pr', 'Lu'), ('Ce', 'Nd', 'Sm '), ('Ce', 'Nd', 'Eu'), ('Ce', 'Nd', 'Gd'), ('Ce', 'Nd', 'Tb'), ('Ce', 'Nd', 'Dy'), ('Ce', 'Nd', 'Ho'), ('Ce', 'Nd', 'Er'), ('Ce', 'Nd', 'Tm'), ('Ce', 'Nd', 'Yb'), ('Ce', 'Nd', 'Lu'), ('Ce', 'Sm', 'Eu'), ('Ce', 'Sm', 'Gd'), ('Ce', ' Sm', 'Tb'), ('Ce', 'Sm', 'Dy'), ('Ce', 'Sm', 'Ho'), ('Ce', 'Sm', 'Er'), ('Ce', 'Sm', 'Tm'), ('Ce', 'Sm', 'Yb'), ('Ce', 'Sm', 'Lu'), ('Ce', 'Eu', 'Gd'), ('Ce', 'Eu', 'Tb'), ('Ce', 'Eu', 'Dy'), ('Ce', 'Eu', 'Ho'), ('Ce', 'Eu', 'Er '), ('Ce', 'Eu', 'Tm'), ('Ce', 'Eu', 'Yb'), ('Ce', 'Eu', 'Lu'), ('Ce', 'Gd', 'Tb'), ('Ce', 'Gd', 'Dy'), ('Ce', 'Gd', 'Ho'), ('Ce', 'Gd', 'Er'), ('Ce', 'Gd', 'Tm'), ('Ce', 'Gd', 'Yb'), ('Ce', 'Gd', 'Lu'), ('Ce', 'Tb', 'Dy'), ('Ce', ' Tb', 'Ho'), ('Ce', 'Tb', 'Er'), ('Ce', 'Tb', 'Tm'), ('Ce', 'Tb', 'Yb'), ('Ce', 'Tb', 'Lu'), ('Ce', 'Dy', 'Ho'), ('C e', 'Dy', 'Er'), ('Ce', 'Dy', 'Tm'), ('Ce', 'Dy', 'Yb'), ('Ce', 'Dy', 'Lu'), ('Ce', 'Ho', 'Er'), ('Ce', 'Ho', 'Tm'), ('Ce', 'Ho', 'Yb'), ('Ce', 'Ho', 'Lu'), ('Ce', 'Er', 'Tm'), ('Ce', 'Er', 'Yb'), ('Ce', 'Er', 'Lu'), ('Ce', 'Tm', ' Yb'), ('Ce', 'Tm', 'Lu'), ('Ce', 'Yb', 'Lu'), ('Pr', 'Nd', 'Sm'), ('Pr', 'Nd', 'Eu'), ('Pr', 'Nd', 'Gd'), ('Pr', 'N d', 'Tb'), ('Pr', 'Nd', 'Dy'), ('Pr', 'Nd', 'Ho'), ('Pr', 'Nd', 'Er'), ('Pr', 'Nd', 'Tm'), ('Pr', 'Nd', 'Yb'), ('Pr', ' Nd', 'Lu'), ('Pr', 'Sm', 'Eu'), ('Pr', 'Sm', 'Gd'), ('Pr', 'Sm', 'Tb'), ('Pr', 'Sm', 'Dy'), ('Pr', 'Sm', 'Ho'), ('Pr ', 'Sm', 'Er'), ('Pr', 'Sm', 'Tm'), ('Pr', 'Sm', 'Yb'), ('Pr', 'Sm', 'Lu'), ('Pr', 'Eu', 'Gd'), ('Pr', 'Eu', 'Tb'), (' Pr', 'Eu', 'Dy'), ('Pr', 'Eu', 'Ho'), ('Pr', 'Eu', 'Er'), ('Pr', 'Eu', 'Tm'), ('Pr', 'Eu', 'Yb'), ('Pr', 'Eu', 'Lu'), (' Pr', 'Gd', 'Tb'), ('Pr', 'Gd', 'Dy'), ('Pr', 'Gd', 'Ho'), ('Pr', 'Gd', 'Er'), ('Pr', 'Gd', 'Tm'), ('Pr', 'Gd', 'Yb'), ('Pr', 'Gd', 'Lu'), ('Pr', 'Tb', 'Dy'), ('Pr', 'Tb', 'Ho'), ('Pr', 'Tb', 'Er'), ('Pr', 'Tb', 'Tm'), ('Pr', 'Tb', 'Yb'), ('Pr', 'Tb', 'Lu'), ('Pr', 'Dy', 'Ho'), ('Pr', 'Dy', 'Er'), ('Pr', 'Dy', 'Tm'), ('Pr', 'Dy', 'Yb'), ('Pr', 'Dy', 'Lu'), ('Pr', 'Ho', 'Er'), ('Pr', 'Ho', 'Tm'), ('Pr', 'Ho', 'Yb'), ('Pr', 'Ho', 'Lu'), ('Pr', 'Er', 'Tm'), ('Pr', 'Er', 'Yb'), ('Pr', 'Er', 'Lu'), ('Pr', 'Tm', 'Yb'), ('Pr', 'Tm', 'Lu'), ('Pr', 'Yb', 'Lu'), ('Nd', 'Sm', 'Eu'), ('Nd', 'Sm', 'Gd '), ('Nd', 'Sm', 'Tb'), ('Nd', 'Sm', 'Dy'), ('Nd', 'Sm', 'Ho'), ('Nd', 'Sm', 'Er'), ('Nd', 'Sm', 'Tm'), ('Nd', ' Sm', 'Yb'), ('Nd', 'Sm', 'Lu'), ('Nd', 'Eu', 'Gd'), ('Nd', 'Eu', 'Tb'), ('Nd', 'Eu', 'Dy'), ('Nd', 'Eu', 'Ho'), (' Nd', 'Eu', 'Er'), ('Nd', 'Eu', 'Tm'), ('Nd', 'Eu', 'Yb'), ('Nd', 'Eu', 'Lu'), ('Nd', 'Gd', 'Tb'), ('Nd', 'Gd', 'D y'), ('Nd', 'Gd', 'Ho'), ('Nd', 'Gd', 'Er'), ('Nd', 'Gd', 'Tm'), ('Nd', 'Gd', 'Yb'), ('Nd', 'Gd', 'Lu'), ('Nd', ' Tb', 'Dy'), ('Nd', 'Tb', 'Ho'), ('Nd', 'Tb', 'Er'), ('Nd', 'Tb', 'Tm'), ('Nd', 'Tb', 'Yb'), ('Nd', 'Tb', 'Lu'), (' Nd', 'Dy', 'Ho'), ('Nd', 'Dy', 'Er'), ('Nd', 'Dy', 'Tm'), ('Nd', 'Dy', 'Yb'), ('Nd', 'Dy', 'Lu'), ('Nd', 'Ho', ' Er'), ('Nd', 'Ho', 'Tm'), ('Nd', 'Ho', 'Yb'), ('Nd', 'Ho', 'Lu'), ('Nd', 'Er', 'Tm'), ('Nd', 'Er', 'Yb'), ('Nd', ' Er', 'Lu'), ('Nd', 'Tm', 'Yb'), ('Nd', 'Tm', 'Lu'), ('Nd', 'Yb', 'Lu'), ('Sm', 'Eu', 'Gd'), ('Sm', 'Eu', 'Tb'), ( 'Sm', 'Eu', 'Dy'), ('Sm', 'Eu', 'Ho'), ('Sm', 'Eu', 'Er'), ('Sm', 'Eu', 'Tm'), ('Sm', 'Eu', 'Yb'), ('Sm', 'Eu', ' Lu'), ('Sm', 'Gd', 'Tb'), ('Sm', 'Gd', 'Dy'), ('Sm', 'Gd', 'Ho'), ('Sm', 'Gd', 'Er'), ('Sm', 'Gd', 'Tm'), ('Sm ', 'Gd', 'Yb'), ('Sm', 'Gd', 'Lu'), ('Sm', 'Tb', 'Dy'), ('Sm', 'Tb', 'Ho'), ('Sm', 'Tb', 'Er'), ('Sm', 'Tb', 'Tm' ), ('Sm', 'Tb', 'Yb'), ('Sm', 'Tb', 'Lu'), ('Sm', 'Dy', 'Ho'), ('Sm', 'Dy', 'Er'), ('Sm', 'Dy', 'Tm'), ('Sm', 'D y', 'Yb'), ('Sm', 'Dy', 'Lu'), ('Sm', 'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', 'Yb'), ('Sm', 'Ho', 'Lu'), (' Sm', 'Er', 'Tm'), ('Sm', 'Er', 'Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', 'Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', 'Yb', ' Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', ' Gd', 'Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('E u', 'Tb', 'Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', 'Dy', 'Tm'), ('Eu', 'Dy', 'Yb'), ('Eu', 'Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', 'Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'T m'), ('Eu', 'Er', 'Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', 'Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', 'Yb', 'Lu'), ('Gd', 'Tb ', 'Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', 'Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', 'Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', 'Dy', 'Yb'), ('Gd', 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', 'Tm'), ('Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), ('Gd', 'Er', 'Tm'), ('Gd', 'Er', 'Yb'), ('Gd', 'Er', ' Lu'), ('Gd', 'Tm', 'Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', 'Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', ' Dy', 'Tm'), ('Tb', 'Dy', 'Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', 'Yb'), (' Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', 'Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', 'Yb'), ('Tb', 'Tm', 'Lu' ), ('Tb', 'Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', 'Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', 'Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', 'Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', 'Yb', 'Lu'), ('Ho', 'Er', 'Tm'), ('Ho', 'Er', 'Yb'), ('Ho', 'Er', 'Lu'), ('Ho', 'Tm', 'Yb'), ('Ho', 'Tm', 'Lu'), ('Ho', 'Yb', 'Lu'), (' Er', 'Tm', 'Yb'), ('Er', 'Tm', 'Lu'), ('Er', 'Yb', 'Lu'), ('Tm', 'Yb', 'Lu') 3. Example Verification methodology 3: this methodology expands on Verification methodology 2 by the use of naturally occurring microbial cation exchangers, including bacteria and fungi.i. As above but right before step vii (unsealing samples in laboratory), add the following steps:| ii. Lyse the microbes. For example, autoclave each sample-containing beaker for steam sterilization at 250 °F at 15 psi for 15 minutes. This may lyse any microbes and cause an active release of bio-adsorbed metals.| iii. Let sample-containing beakers cool to room temperature before proceeding.| iv. The filter in step (ix) may now act to additionally remove any larger aggregates of microbial cell suspensions that did not lyse in the autoclaving process.| v. The added EDTA in step (x) in Verification Methodology 2 may act to additionally chelate any REEs that are complexed to the cell wall or organic molecules of the microbial genetic material (as a result of cell lysis).| vi. In conjunction, verification methodology 3 provides a protocol to achieve full recovery of REEs that were retained in the top 10 cm of soil due to the following biogeochemical processes:1. Mineral surface interface complexation.| 2. The cation exchange capacity inherent to soils due to organic matter.| 3. Microbially mediated surface biosorption and/or active biological absorption pathways including but not limited to REE-aqueous complexation with internal genetic material of individual microbial cells found in natural soils and sediments. B. Example systems and methods to enhance the agronomic performance and ecosystem co-benefits:In these non-limiting embodiments, product formulations are detailed that improve the soil quality for improved agronomic applications as well as embodiments that specify improvements on crop health and an ability for plants to protect themselves from pathogens.| Addition of macronutrients that enhance the agronomic benefits of the applied mineral. Example: addition of elemental 1-5% by weight formulation K or Ca or inexpensive REE such as La to improve use cases of pulverized Mg2SiO4 by improving the nutrient balance of the soil to match the needs of actively growing plants. Application rates for K and Ca may range from 50-100 ppm and lanthanide addition rates may range from 1-50 ppm.| The 1-5% by volume addition of slow-release acidifiers in the form of elements that maintain the acidity of the soil despite the tendency of the applied mineral to reduce soil acidity in the weathering process. Example: addition of minerals with Al (such as gibbsite, Al(OH)3) or S (such as gypsum, CaSO4)-2H2O), in a rate of 1-10% by weight of total formulation, which contribute to maintaining soil acidity, and thus maintain high rates of weathering, which counteracts the tendency of forsterite weathering to increase alkalinity, which slows rates of weathering.| The incorporation of additional micronutrients such as zinc (1-5% by weight compared to mineral amendment) to reduce ecosystem losses of phosphorus and downstream ecosystem impacts of phosphate-based fertilizers, such as eutrophication. Phosphates are immobilized via precipitation reactions with the additional zinc metal, so zinc addition slows the transport and reduces mobility of phosphate in the subsoil. As a consequence, phosphate-based fertilizer applications can be performed more safely and with higher confidence that downstream waterways will not form algal blooms and lead to anoxic, uninhabitable waterways for aquatic life. The addition of 1-32 tons/hectare of mineral in conjunction with 1-5% by weight zinc in fields with heavy phosphate application reduces the likelihood of significant phosphate leaching. This also increases nutrient use efficiency, which reduces fertilizer cost to farmers and reduces negative environmental impacts to society. Specifically, phosphate-zinc precipitates become slow-releasing over time due to their immobilization in the soil as a solid phase. This provides longer timeframes for plants to access the phosphate application, reducing the frequency of fertilization.| The method of mixing of different mineral adjuvants to the primary mineral used for carbon removal can be varied, with impacts on performance. In some embodiments, the admixture (e.g., of gypsum and forsterite) could be completely emulsified. In some embodiments, a nutrient, such as urea, could represent a core that is subsequently coated with a shell of silicate mineral used for carbon removal. In some embodiments the silicate mineral could be the core, and the nutrient, such as urea, could be the coating. In each of these cases, the embodiment can be optimized so as to reduce environmental losses of the nutrient, and increase availability to the plant, while providing the acidity necessary for the silicate mineral weathering. In some embodiments, this may represent a "slow release" nutrient that does not mineralize too quickly and is synchronized more favorably with plant demand.| Comminution, or pulverization, may help reproduce the expected kinetics of alkalizers such as pulverized limestone or dolomite, known as aglime. Aglime has well-characterized kinetics originating in the particle size distribution of the product, which are in some jurisdictions legally regulated to meet certain requirements. A representative cross section of dissolution kinetics based on actual aglime mesh size observations is depicted in FIG. 2.|It naturally follows that agronomic performance expectations for silicate minerals used for ERW should follow similar reaction kinetics, particularly in the first year after application, while also meeting the goals for CDR. Thus, an ideal particle size distribution may be tuned to meet this goal. The following shows the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um, such as 90um, which closely approximates the alkalinity release dynamics for aglime.| The small particle sizes produced by pulverization as above are valuable for performance as an aglime substitute and CDR mechanism, but introduce their own set of potential challenges. One potential challenge is that small particle sizes may fall within regulated categories such as PM10 or PM2.5; another potential challenge is the product may not be easily transferred from one vessel to another (so-called "flowability") because it has a tendency to settle into a compact mass; the product may also not be applied uniformly by extant farm equipment; potentially low uniformity application impacts the agronomic performance as well as the sampling density needed for carbon removal verification. In one potential formulation, the product is pelletized after pulverization, using a common binder such as lignosulfate in a 3-5% ratio by weight of the total formulation. The amount of binder may be optimized to improve performance characteristics during transport and application, but minimize the water and energy needed to dissolve the pellet once it is in the field. Pelletizing the product, into a size range of, for example, 0.5 mm to 3 mm increases the flowability; reduces the prevalence of dust, including the risk of asbestos exposure; enables the use of extant crop input application equipment; and improves the evenness of field distribution, which has the agronomic and carbon verification benefits identified. Pelletizing in this size range also ensures that an adequate number of pellets fall onto any land area which may subsequently be sampled for analysis.| A desiccated but living biological compound, such as a mycorrhizal inoculum, may be used to coat the agglomerated and dried pellets, so as to enhance the dissolution of the pellet itself after application. This may be distinct from a fungal adjuvant to the pellet to increase dissolution of the silicate minerals themselves.| To accommodate a range of soil types from acidic to neutral pH, the product may be differentiated into different particle size distributions so as to achieve a consistent rate of weathering across different soil types. For example a consistent rate of weathering may be that the entire applied amount of mineral product weathers in 9 months, allowing a subsequent application every year. To achieve this, an acidic soil may have pellets that contain particles with a modal size on the order of 100 um, while a neutral soil may have pellets that contain particles with a modal size on the order of 10 um. The negative consequence of applying a fine particle in an acidic soil may be that it dissolves too quickly, swinging the pH of the soil too quickly, and altering the nutrient availability severely in the growing plant. The negative consequence of applying a coarse particle in a neutral soil may be that the particle weathers too slowly or is functionally inert, which does not remove carbon as intended, and may subject the farmer or the vendor to risk of clawbacks for payments received for carbon removal. C. Example systems and methods to control or enhance the performance as a securitized carbon removal method:In these non-limiting embodiments, product formulations are described that improve the marketability of pulverized and optionally pelletized mineral amendments as a verifiable carbon removal method, irrespective of their impact on agronomic performance. Such changes in marketability increase the value of the carbon product, for example for detecting and preventing fraud, or increase the dissolution rate (mass per area per year) to accelerate the timing of reapplication, which raises the value in a discounted cash flow analysis. The general scheme is depicted in FIG. 4.| The addition of low cost and inert trace elements, for example 1-5 ppm neodymium or lanthanum, to a mineral amendment, beyond the natural abundances present in the ore body, improves performance in Verification methods 2 and 3. Specifically, the additional elements reduce measurement uncertainty owing to low natural abundance calculations as well as uncertainty owing to variability from the source mineral. Reduction of these uncertainties improves the detectability of true positives and true negatives. This principle could be applied to many potential soil amendments and fertilizers to verify provenance as pertains to legal contracts.| The addition of binders to create aggregations of the ground mineral that could reduce drift, which improves distribution uniformity; reduces potential respiratory health impacts; and/or improves applicability of the applied mineral using commercially available equipment. For example, a biofilm mediating organic compound, such as alginate or chitosan, could be mixed with a pulverized mineral with a particle size of approximately 100 microns to achieve an aggregated pellet size of 1 millimeter. This would maintain the advantages of fine particle size, particularly the high specific surface area (m2/g) that mediates dissolution rate, while offsetting potential limitations outlined above. An example methodology for aggregating ground minerals could include these steps:∘ Dissolve 10 grams of alginate powder into solution to create a 0.5 M - 1.0 M alginic acid solution.| ∘ Heat solution to 80-100 °F to dissolve alginate powder fully if necessary.| ∘ Spray aerosol sized particles of dissolved alginate powder onto the ground rock material in order to create a biofilm-coated rock material. Apply a consistent spray of 100 mL for each 100 gram of rock (1:1 v/w).| ∘ The resulting aggregates may have increased bulk density as well as higher aggregating properties due to van der Waals force attraction between the individual rock particles. Dissolution rates can be modified by non-living organic molecules applied concurrently with the mineral amendment. For example, protonated microbes such as acid-treated Arthrobacter nicotianae can constitute an initial release of protons to attack the ground rock materials' crystal structure. This method of acidification for optimal accelerated weathering of rock material may occur even during winter/cold climate. Because biologically mediated processes can have sharp thresholds, e.g., under freezing conditions, such a chemically controlled process would exhibit greater ability to expedite rock breakdown over a range of environmental conditions. To implement this methodology, we outline the following steps:1) De-frost an aliquot of A. nicotianae in 5 mL of Luria broth for about 24 hours at exactly 30 °C.| 2) Sub-culture into a larger volume of Luria broth at a 1:50 dilution and allow growth for another 24 hours at 30 °C.| 3) During growth steps #1 and 2, cultures may be shaken, for example at 200-220 RPM, for aeration.| 4) After culture has been grown for 48 hours in total, centrifuge the cell suspension.| 5) Collect cell pellet and take a small amount and set it aside. Weigh wet weight, dry at 60 °C overnight, and weigh dry amount to obtain wet : dry conversion.| 6) Develop an OD600 to wet weight to dry weight conversion by taking 5 varying amounts of wet aliquots of wet biomass and measuring optical density given its known wet mass. Wet aliquots may have a mass of about 1, 4, 8, 12, 16 wet grams and be suspended in 100 mL of DI water.| 7) Wash cells in 0.1 M NaCl solution.a. Centrifuge cells+growth media at 4000xg.| b. Carefully pour out LB broth.| c. Add 0.1 M NaCl solution.| d. Centrifuge cells+NaCl solution at 4000xg.| e. Carefully pour out NaCl solution. 8) Protonate the cells while wet.a. Re-suspend the wet biomass in an acidic (e.g., pH 3.0) solution using a dilute hydrochloric acid solution (0.001-0.01 M).| b. Centrifuge cells+HCl solution at 4000xg.| c. Carefully pour out solution.| d. Repeat steps (a)-(c) a total of three times.| e. Dry cells in an oven at 80-100 °C for 48 hours.| f. Grind cells using a mortar/pestle to achieve a powder form. 9) Mix 5% w/w of dry cell powder with the ground rock material.| 10) When this particular rock material+cell powder mixture is applied to agricultural soils, the irrigation or rainfall will re-apply moisture and allow the pre-protonated, re-wet biomass to release their protons. This will ultimately induce a local acidity effect on the rock particle (molecular) level to accelerate rock crystal lattice breakdown. The cells act as biodegradable transporters that are also benign to the natural soil environment. (EP4256520)|Cross Reference to Related Applications|[0001] The present applications claims the priority benefit of U.S. Provisional Patent App. Serial No. 63/322,672, filed March 23, 2022; U.S. Provisional Patent App. Serial No. 63/289,395, filed December 14, 2021; and U.S. Provisional Patent App. Serial No. 63/213,398, filed, June 22, 2021.|Background|[0002] The last several years have witnessed a maturation of carbon markets from lightly scrutinized voluntary markets largely serving to provide positive marketing collateral to familiar consumer brands to rigorous compliance markets with proof-of-performance requirements often involving government and quasi-governmental regulators. There have also been a number of comprehensive proposals for decarbonization of the entire US economy, combining energy production, transportation, cement production, and agriculture. These proposals have included carbon dioxide removal (CDR) techniques as an essential component of the decarbonization plan, with a supportive ecosystem of science, policy, and project evaluation criteria. Within the diverse scope of decarbonization efforts, including renewable energy, biofuel, nature-based solutions, and more technical CDR techniques like direct air capture (DAC), The Oxford Principles have developed a taxonomy for categorizing diverse decarbonization strategies. This taxonomy distinguishes between avoided emissions (for instance, conversion of fossil fuel power to renewable power) and negative emissions (for instance direct air capture); distinguishes between avoided emissions that require storage (for instance carbon capture from a point source and sequestration into the ground) and those that do not require storage (the conversion to renewable energy); and the duration of the storage if so required (for instance, short lived forest carbon sequestration from delayed harvests versus storage of captured carbon in geological formations).|[0003] A number of for-profit and non-profit organizations have emerged that employ the Oxford Principles to evaluate proposals, particularly around the rigorous quantification across categories (Table 1). This, in essence, is the scorecard that projects will have to compete on to find acceptance in the industry. All other things equal, cost ends up being the primary driver, but quality is also a key consideration. Thus, historically buyers have been drawn to nature-based solutions that cost between $5-20/tCO2 e (e.g., Corteva Carbon, Indigo Carbon), versus direct air capture projects that cost >$500/tCO2 e (e.g., ClimeWorks). However, there are challenges to these nature-based solutions: recently these nature-based solutions have been subject to intense scrutiny for "gaming" the rules or otherwise failing to deliver prospective rewards. Among the technological solutions, there are a different set of challenges: rigor has been strong, but the reduction in price proportional to increase in deployment has been slow, and the ultimate price of DAC is not expected to drop below $150/tCO2e (Keith et al 2018, https://doi.org/10.1016/j.joule.2018.05.006). In light of these challenges, we have developed a technology around "enhanced rock weathering" (ERW), in which silicate minerals are weathered in acidic soil solution, thus driving the uptake of additional CO2 into dissolved inorganic carbon (DIC) in the soil solution. Our experimental work, life cycle analysis, and techno-economic modeling have indicated that ERW provides the permanence, additionality, and rigorous quantification of a DAC project, the large volume of a carbon capture and storage (CCS) project, and the unit economics of a nature based solution, thus creating a new tool to meet net-zero goals.|Details of Enhanced Rock Weathering|[0004] In "enhanced rock weathering" (ERW), silicate minerals are weathered by CO2 from the ambient air which has been dissolved into water, reacting to produce dissolved inorganic carbon that is ultimately stored in the ocean as depicted in FIGS. 1 and 2.|Background Geochemistry|[0005] The role of silicate rock weathering in maintaining the CO2 balance of the atmosphere has been recognized for decades, first outlined by renowned chemist Harold Urey in the 1950s. The basic premise of the Urey reaction is that continental collisions release CO2 to the atmosphere from volcanoes, and bring Mg- and Ca-bearing silicate rocks to the surface. The rainwater (H2O) that falls upon these rocks is mildly acidic, as atmospheric CO2 has dissolved in it and formed carbonic acid (H2CO3). For forsterite, the weathering reaction takes place following the form:|        Mg2SiO4 + 4 H2O + 4 CO2 → 2 Mg2+ + 4 HCO3- + 4 H4SiO4|[0006] In this reaction, one mole of forsterite consumes four moles of CO2, so two negatively charged bicarbonate HCO3- are created for every one divalent Mg2+ weathered. Given the molecular weight of forsterite (140 g/mol) and the molecular weight of CO2 (44 g/mol), weathering one metric ton of forsterite removes 1.25 metric tons of CO2 from the atmosphere. In general, such a formula can be used to define the "mineral potential" of a silicate based on its elemental composition: | where V is the valence of the cation (2 for Mg and Ca) and MW is the molecular weight.|[0007] The rate of weathering is determined by the surface area of the mineral, the acidity (pH) of the soil solution, the temperature of the solution, the availability of CO2 reagent in solution, and the rate of removal of the reaction products by water. One of the key insights into the potential of "enhanced" rock weathering is that the rate of reaction, and thus CO2 removal, can be greatly accelerated by increasing the surface area by pulverization into a fine powder (e.g., less than 100 um), incorporating into an acidic environment (e.g., pH less than 6) with abundant CO2 present, and with steady water flux to remove reaction products to maintain acidity. While this formula defines the potential amount of CO2 that may be removed by weathering, it does not speak to the rate; ancient rock formations testify that the rate of weathering can be extremely slow.|[0008] The relationship between silicates (like Mg2SiO4) and dissolved carbonates (like HCO3-) is not necessarily intuitive, as the carbonate system of water involves a number of coupled reactions. Atmospheric CO2 dissolves into water according to an exchange coefficient:|        CO2(aq) = H2CO3 = KCO2 * pCO2|[0009] Technically pCO2 is "fugacity" that represents its activity, but, as used herein, it is more or less equivalent to its partial pressure, and KCO2 is the Henry's law coefficient that determines the aqueous CO2 in equilibrium with the atmosphere. This aqueous CO2 in turn hydrates with H2O to become carbonic acid (H2CO3), which dissociates to become bicarbonate (HCO3-) and carbonate (CO32-):|        H2CO3 ↔ HCO3- + H+|        HCO3- ↔ CO32- + H+|[0010] These equilibrium reactions are defined by K1 and K2, the first and second carbonate system dissociation constants. pK1 and pK2 are about 5.9 and about 9.4 at STP, so greater than 99% of the charge in the dissolved carbonates is HCO3-.|[0011] The carbonates are the largest constituents of total alkalinity, which is defined as the charge imbalance between weak acids (proton acceptors) minus proton donors:|        TA = [HCO3-] + 2 · [CO32-] + [OH-] - [H+]|[0012] There is an alternative definition of total alkalinity as the charge imbalance between conserved cations and conserved anions:|        TA = [Na+] + 2 [Mg2+] + 2 [Ca2+] + [K+] + ... - [Cl-] - 2 [SO42-] - [NO3-]|[0013] These two expressions are always equal (i.e. the charges balance). This means that an added Mg or Ca into soil solution will increase in HCO3- to balance the charge. We describe an analytical solution to compute how much carbon is taken up per unit of additional Mg or Ca. If we first define DIC as the sum of H2CO3, HCO3-, and CO32-, and make use of the equilibrium equations above (defining H+ as "h" and H2CO3 as "s"): |[0014] And formulate TA using the same convention: |[0015] With these definitions in place, we can develop an estimate of dDIC/dTA. First, we compute the derivative dTA/dh: |[0016] Next we compute the derivative dDIC/dh: |[0017] Finally we multiply dDIC/dh by the inverse of dTA/dh to calculate dDIC/dTA: |[0018] At the pH found in soils, each Mg or Ca is matched by two carbon atoms. In all circumstances, raising alkalinity results in increased pH. This is particularly important in marine settings, where ocean acidification from increased atmospheric CO2 can be ameliorated by this export of alkalinity from land.|[0019] The potential for ERW as a commercial enterprise is limited by some fundamental issues:| A. The total amounts of mineral transformation and carbon removal should be verifiable empirically. The verification methods described below may be low cost at scale, can be performed at arm's length by a 3rd party, and may have safeguards to eliminate fraud.|[0020] Additionally, the commercial potential for ERW could be enhanced by a number of different features. Embodiments may include:| B. Processes and modifications of the engineered mineral product that enhance the agronomic performance and ecosystem co-benefits of the engineered mineral.| C. Processes and modifications of the engineered mineral product that control or enhance the mineral dissolution rate of the engineered mineral in soil environments and thus the rate of removal of CO2.| C. Paulo et al, Applied Geochemistry, 2021, 219, 104955, discusses evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralisation.| N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809 discusses carbon dioxide efficiency of terrestrial enhanced weathering and determination of effective carbon dioxide sequestration.|Brief Description of the Drawings|[0021] FIG. 1 is a drawing illustrating the enhanced rock weathering cycle.| FIG. 2 is a graph depicting the effect of comminution on dissolution kinetics for a silicate.| FIGS. 3A to 3D are graphs depicting the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um which closely approximates the alkalinity release dynamics for aglime.| FIG. 4 is a drawing illustrating the general scheme for a verified enhanced rock weathering cycle.|Detailed Description|[0022] Summary: The following described methodologies can establish one version of a verification scheme that will demonstrate the transformation of the applied rock material and the subsequent carbon removal into secure geologic reservoirs as evidenced by observations collected from the soil. One set of methods (A) can measure the production of free ions from the applied material and the transport of those ions outside of a control volume as a direct measure of the amount of weathering and thus total carbon dioxide equivalent isolated from the atmosphere. Furthermore, as the elemental inputs into the soil induced by enhanced rock weathering can have significant effects on the soil geochemistry, methods in (B) describe systems and versions that can enhance the agronomic performance of the soil amendment and increase ecosystem co-benefits. Lastly, methods in (C) elaborate on versions that control and enhance the mineral dissolution rate, which increases the financial performance of enhanced rock weathering technology in the marketplace.| A. Systems and methods for monitoring and verification:Described below are several example methodologies for quantifying the rate and extent of mineral transformation and carbon removal, which are referred to as "verification methodologies".1. Example Verification methodology 1:a. A cation exchange resin and/or an anion exchange resin are packaged into a physical embodiment (such as a 5 cm diameter tube, 5cm in length, placed 30 cm below the soil surface) that allows vertical transport of fluids but not horizontal transport.| b. Commercial ion exchange resins are pre-equilibrated in such a way that their selectivity is high for the relevant ions, but their capacity is also sufficiently high such that saturation is minimized. This technology may allow for effective deployment for long periods of time, allowing passage of up to 4000 mm of moisture through the tube, without becoming saturated with respect to the ions of interest.| c. The ions of interest are restricted to divalent cations (Mg2+, Ca2+), carbonate species (HCO3- and CO32-), and silicic acid (H4SiO4), important weathering products of preferred mineral soil amendments, such as ultramafic rocks, blast furnace slag, and other naturally occurring or industrial silicate minerals with high Mg and Ca content.| d. Three pre-equilibrated tubes are emplaced fully under the soil below a control depth (e.g., 30 cm, a typical depth of cultivation). This may be done by removing the top 30 cm soil with a shovel or auger, then gently placing the tube in the created void space. Following a certain period of time post-surface application of mineral soil amendment (e.g., 9 to 12 months after application), the tubes are retrieved, and the ions captured within the resin exchanges are measured using standard methodologies, such as ICP-OES and ICP-MS based concentration measurements. Three tubes are used to determine standard deviation error in triplicate.| e. By the principle of charge balance and known thermodynamic reactions taking place in the top 30 cm of soils, the amount of carbonate can be inferred purely from the measurement of cations, under certain assumptions and auxiliary geochemical data. By the addition of more specific anion exchange resins, such as styrenedivinylbenzene, these assumptions can be avoided to get a more precise answer. The increase in cation concentration in the subsurface soil pore water allows for the stoichiometric determination of carbon removal from the gas phase (ambient air).| f. The total carbon dioxide removed during the deployment period may be estimated as equal to the molecular mass of CO2 (44 g/mol) multiplied by the sum of the number of moles of carbonate and two times the number of moles of bicarbonate, multiplied by the area on which mineral was applied to the field, divided by the cross-sectional area of the tube.| g. Direct measurement of aqueous bicarbonate and carbonate species, which are the most readily available forms of carbon induced by a gas exchange of carbon dioxide with the soil pore water, may be conducted using the specified anion exchange resin above. The expression as described in clause (f) explains the calculation used to convert this direct measurement of carbon to an absolute value of carbon dioxide removed during a specified application period.| h. Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.| i. However, potential disadvantages may include the need for manufacturing (and its attendant demand for working capital); devices may occasionally be defective; emplacement of a device may alter the flow paths of water, which in turn alters the inferred ion fluxes; emplacement of a device may depend on the user; the knowledge of the location of emplacement may invite manipulation by a stakeholder involved in a carbon transaction; and others. 2. Example Verification methodology 2:a. The principle behind Verification methodology 2 is that minerals applied for purposes of enhanced rock weathering contain, in addition to the elements outlined above that participate in the weathering reaction (i.e., magnesium, calcium, iron, silicon, oxygen, hydrogen), additional elements in trace amounts. These additional trace elements (TEs) might include rare earth elements (REEs), rare metals (RM), other transition metals (TMs), or a combination thereof. Unlike the primary weathering products that are readily dissolved in solution and lost by leaching, some TEs are strongly bound to mineral and biological surfaces and do not readily leach from the soil control volume (e.g., the top 10 to 30 cm of soil), and are not removed by plants at the concentrations present in our applied rock. These strongly bound trace elements are referred to herein as immobile trace elements (ITEs). Thus, a measure of cumulative cation flux and carbon removal can be computed by comparing the ratio of the lost weathering products, such as magnesium, to ITEs, after accounting for background concentrations of ITEs in the initial soil.| b. As used herein, rare earth elements include scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), lutetium (Lu) or a combination thereof. As used herein, rare metals include beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), zirconium (Zr), or a combination thereof. As used herein, transition metals include nickel (Ni), chromium (Cr), and zinc (Zn) among others and may include a combination of transition metals.| c. An approach based on ITEs depends on the degree of immobility of the element in soil environments, the time horizon after which the ITEs will be measured to estimate carbon removal, the abundance of ITEs in both the soil and the mineral added, and the analytical chemistry used to measure this abundance. An analytical technique that has low detectability thresholds for slightly mobile elements could be sufficient for relatively abundant (e.g., parts per thousand to parts per million) elements over short time horizons (e.g., weeks to months). On the other hand, a different analytical technique could be used over longer time horizons, which in turn could involve quantification of very immobile elements that are present in much lower abundance (e.g., parts per billion to parts per trillion). The approach may be chosen based at least in part on cost, which ITEs are actually conserved, over which time horizons, as well as the performance of the analytical performance used.| d. The relative proportions of ITEs in a sample (rock or soil) constitute a type of unique fingerprint of the material. Because the cost of pure ITEs is large, and the analytical chemistry is not widely available, there is a significant barrier to engineering a fraudulent sample to reproduce the native ITE fingerprint of a mineral soil amendment. Thus, it would be challenging for a stakeholder in a carbon exchange transaction to generate a result that produces the anticipated result (a high or low amount of carbon removal) while also matching the ITE fingerprint generated by a bona fide sample. This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).| e. Verification Methodology 2 (VM2) has advantages over Verification Methodology 1 (VM1) in that it avoids the need for the use of a device, which avoids altering the soil hydrology or physical environment in a way that would impact the observed elemental analysis.| f. VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.| g. VM2 does, however, include measurement techniques that are less widely available; requires specialized instruments and personnel; requires additional boundary conditions to compute carbon flux (e.g., pre-application soil and rock elemental analysis); and employs assumptions as to the relationship between cation flux and carbon flux.| h. Like VM1, VM2 uses the total amount of mineral applied and the field area, which could be measured, for example, using a digital as-applied map commonly accompanying crops input machinery, or truck weights before and after mineral delivery. This will be referred to as the nominal application rate (ARnominal).| i. There are four main calculations in VM2. To the extent any one of these factors is known unambiguously from other sources, each step in VM2 could be used in isolation from the others.i. Classify, using ITE fingerprinting, whether a soil has had a specific mineral applied, which may be asserted by an entity wishing to make a claim;| ii. Calculate, using ITE fingerprinting, what the actual mineral application rate (ARactual) for a specific soil sample was, which will necessarily differ in a systematic or random way from the average rate for the entire field;| iii. Calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the application rate in (ii) above;| iv. Calculate, using the fraction computed in (iii) and the mineral potential (Equation 1) computed for the feedstock identified in (i) above, the amount of carbon dioxide removed. j. In one non-limiting embodiment, the verification methodology to classify whether the claimed mineral applied is the actual mineral applied is as follows:i. Collect a sample from mineral to be applied, place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Mineral Amendment.| ii. Prior to mineral application, collect a 20 g sample from cultivated zone of soil (typically at around 30 cm, such as in a range of 0 cm to 30 cm), place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Soil A.| iii. Subsequent to mineral application, collect a 20 g sample the same control zone as soil A, and store under similar conditions. Label as Soil B. Soil B could be sampled immediately after mineral application or at a later time (e.g., months to years afterwards).| iv. Characterize the elemental composition of Mineral Amendment, Soil A, and Soil B. Example approaches to characterizing the elemental composition are described in (v) and (vi).| v. One approach to measuring the elemental composition is as follows:1. In a laboratory setting, unseal the soil samples and place 10 grams of Soil A and Soil B in two separate beakers.| 2. Dissolve the solids in strong acid. For example, add 21 mL of strong 1.0 M hydrochloric acid and 7 mL of strong 1.0 M nitric acid (total 28 mL acid) to each beaker of sterilized soil and stir rigorously until solids are dissolved.| 3. Filter the sample-containing beakers first through a 1- to 5-micron water filter cartridge followed by an attached 10 to 20 cm column cation exchange resin at a sufficiently slow flow rate of, for example, 1 to 5 mL/min. This combination of a water filter with a cation exchange column has been engineered for optimal performance with soils under consideration. Specifically, the 5-micron water filter cartridge separates out any larger particles, allowing for the smaller particles to exchange its bound metals with the subsequent cation exchange resin.| 4. Flush copious amounts (e.g., 100-200 mL) of 0.5 to 1.0 M chelator such as, for example, ethylenediaminetetraacetic acid (EDTA) at 1-5 mL/min through the used filters into their respective filtrates. This may collect any additional metals that were still adhered to the filters.| 5. Send filtrate A (resultant sample from Soil A) and filtrate B (resultant sample from Soil B) to an analytical laboratory for analysis on an inductively coupled plasma mass spectrometer (ICP-MS). Measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3.| 6. The ICP-MS may be set to detect magnesium concentrations and the following 17 elements on a high ppb or low ppm detection level: Yttrium, Scandium, Lanthanum, Cerium, Praseodymium, Neodymium, Promethium, Samarium, Europium, Gadolinium, Terbium, Dysprosium, Holmium, Erbium, Thulium, Ytterbium, Lutetium. Classify light rare earth elements (LREEs) as yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium. Classify heavy rare earth elements (HREEs) as europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium. Send an isolated rock material sample for ICP-MS analysis. Similar to the filtrate analyses, measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3. vi. Another approach to measuring the elemental composition is as follows:1. Calibrate a portable XRF instrument for particularly low detection limit of ITEs using a calibration standard (such as Bruker proprietary Geo calibration + custom ITE standards).| 2. Use the portable XRF instrument to analyze the Rock Material and Soil A for ITEs (as identified in Verification methodology 2), reporting the instrumental error (2 standard deviations) as well.| 3. Use the portable XRF instrument to analyze Soil B for ITEs, reporting the instrumental error (2 standard deviations) as well. vii. Once the above elemental composition has been determined, calculate the difference for every element between Mineral Amendment and Soil A, resulting in a vector of differences vrock. Likewise, compute the difference for every element between Soil B and Soil A, resulting in a vector of differences vsoil. To improve performance, each element may be divided by an individual factor, such as the detection threshold, or the instrumental uncertainty, or the elemental composition of a reference material. Another means to improve performance would be to sum a subset of the elements or several distinct subsets of elements before computing vrock and vsoil. Another means to improve performance would be to compute indices of these summed subsets of elements, for example the ratio of the light REEs to the heavy REEs, before computing vrock and vsoil.| viii. Compute the dot product of vrock and vsoil. If the value of this dot product is close to 1 (e.g., within a threshold value), then the Soil B is positively classified as having the Mineral Amendment. If the value of the dot product is less than 1 minus a threshold value, then Soil B is negatively classified as not having the Mineral Amendment.| ix. The threshold value may be determined using a variety of means, for example the half-angle between the dot product of vrock and vsoil and any other known vrock and vsoil; or using a Monte Carlo simulation of vrock and vsoil that accounts for known sources of uncertainty including instrumental error, variation in rock elemental analysis, or variation of soil elemental analysis. k. In one non-limiting embodiment, the verification methodology to calculate the actual mineral application rate (ARactual) for a specific soil sample is as follows:i. Characterize the elemental composition the elemental composition of Mineral Amendment, Soil A, and Soil B as above. Note that there could be different analytical chemistry employed if, for example, rapid and inexpensive XRF analysis was used for classification soon after application, and slower and more costly ICP analysis may be used to estimate application rates.| ii. Compute the differences in elemental composition as above, potentially including similar performance enhancements such as normalizing by factors specific to each element, summing across subsets of elements, and computing indices such as the ratio of light REEs to heavy REEs. Such transformed and summed variables for a sample will be referred to generically as ΣITEsample.| iii. The actual application rate of the sample can be calculated using the following expression: l. In one non-limiting embodiment, the verification methodology to calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the actual mineral application rate (ARactual) as follows:i. The amount of divalent cations applied (DCapplied) can be calculated by the proven identity of the mineral additive and the actual application rate: where divalent cations are generally restricted in this context to Mg and Ca, and Mgmineral and Camineral is the fractional composition of the mineral additive.| ii. The amount of divalent cations remaining (DCremain) in the soil could be estimated using the same elemental analysis as previously (if, for example, ICP-MS was used), or determined from the same sample using a different analysis (if, for example XRF was used and Mg was not measured).| iii. The fractional progress of carbon dioxide removal (CDR) can be estimated by the ratio of remaining divalent cations to applied divalent cations: m. In one non-limiting embodiment, the verification methodology to calculate the amount of carbon dioxide removed from the control volume is as follows:i. Assembling MP, fCDR , ARnominal and the land area applied, the total carbon dioxide removal is: n. While Verification Methodology 2 presented herein provides a broad framework for the detection and application of soil-bound ITEs to estimate long-term geologic carbon drawdown, the efficacy of the approach can also be improved through the focus on specific subsets of ITEs. Non-limiting embodiments of such improvements are listed below:i. The ITEs specified in equation 2, e.g., (ΣITEssoil B), may in fact be represented not by the full summation of 17 REEs but instead by the use of only LREEs or the use of only HREEs, as defined in clause xii. Such a calculation would mean the sum of only LREEs in the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium) or the sum of only HREEs in the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium).| ii. Within the use of only LREEs for the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium), some LREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual LREEs are selected. For example, the subset may include three LREEs. The calculation (equation 2) is conducted for each of the 3 LREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 LREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [yttrium, scandium, lanthanum], [cerium, lanthanum, neodymium], [cerium, neodymium, samarium], [yttrium, cerium, neodymium], [scandium, neodymium, samarium].| iii. Within the use of only HREEs for the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium), some HREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual HREEs are selected. For example, the subset may include three HREEs. The calculation (equation 2a) is conducted for each of the 3 HREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 HREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [europium, gadolinium, terbium], [europium, terbium, dysprosium], [dysprosium, erbium, ytterbium], [europium, erbium, ytterbium], [europium, dysprosium, erbium].| iv. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual REEs are selected. For example, the subset may include three REEs Chart 1 represents a non-limiting list of REE triplicates that may enhance the efficacy of this C drawdown calculation.Chart 1. A non-limiting list of 455 REE triplicates that can be used to effectively triangulate a C drawdown estimation|('Y', 'La', 'Ce'), ('Y', 'La', 'Pr'), ('Y', 'La', 'Nd'), ('Y', 'La', 'Sm'), ('Y', 'La', 'Eu'), ('Y', 'La', 'Gd'), ('Y', 'La', 'Tb'), ('Y', 'La', 'Dy'), ('Y', 'La', 'Ho'), ('Y', 'La', 'Er'), ('Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), ('Y', 'Ce', 'Pr'), ('Y', 'Ce', 'Nd'), ('Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eu'), ('Y', 'Ce', 'Gd'), ('Y', 'Ce', 'Tb' ), ('Y', 'Ce', 'Dy'), ('Y', 'Ce', 'Ho'), ('Y', 'Ce', 'Er'), ('Y', 'Ce', 'Tm'), ('Y', 'Ce', 'Yb'), ('Y', 'Ce', 'Lu'), (' Y', 'Pr', 'Nd'), ('Y', 'Pr', 'Sm'), ('Y', 'Pr', 'Eu'), ('Y', 'Pr', 'Gd'), ('Y', 'Pr', 'Tb'), ('Y', 'Pr', 'Dy'), ('Y', 'Pr ', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', 'Yb'), ('Y', 'Pr', 'Lu'), ('Y', 'Nd', 'Sm'), ('Y', 'Nd', 'E u'), ('Y', 'Nd', 'Gd'), ('Y', 'Nd', 'Tb'), ('Y', 'Nd', 'Dy'), ('Y', 'Nd', 'Ho'), ('Y', 'Nd', 'Er'), ('Y', 'Nd', 'Tm' ), ('Y', 'Nd', 'Yb'), ('Y', 'Nd', 'Lu'), ('Y', 'Sm', 'Eu'), ('Y', 'Sm', 'Gd'), ('Y', 'Sm', 'Tb'), ('Y', 'Sm', 'Dy'), ('Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), ('Y', 'Sm', 'Tm'), ('Y', 'Sm', 'Yb'), ('Y', 'Sm', 'Lu'), ('Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), ('Y', 'Eu', 'Dy'), ('Y', 'Eu', 'Ho'), ('Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), ('Y', 'Eu', 'Yb'), ('Y ', 'Eu', 'Lu'), ('Y', 'Gd', 'Tb'), ('Y', 'Gd', 'Dy'), ('Y', 'Gd', 'Ho'), ('Y', 'Gd', 'Er'), ('Y', 'Gd', 'Tm'), ('Y', ' Gd', 'Yb'), ('Y', 'Gd', 'Lu'), ('Y', 'Tb', 'Dy'), ('Y', 'Tb', 'Ho'), ('Y', 'Tb', 'Er'), ('Y', 'Tb', 'Tm'), ('Y', 'Tb ', 'Yb'), ('Y', 'Tb', 'Lu'), ('Y', 'Dy', 'Ho'), ('Y', 'Dy', 'Er'), ('Y', 'Dy', 'Tm'), ('Y', 'Dy', 'Yb'), ('Y', 'Dy', 'Lu'), ('Y', 'Ho', 'Er'), ('Y', 'Ho', 'Tm'), ('Y', 'Ho', 'Yb'), ('Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), ('Y', 'Er', 'Y b'), ('Y', 'Er', 'Lu'), ('Y', 'Tm', 'Yb'), ('Y', 'Tm', 'Lu'), ('Y', 'Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', 'Nd' ), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', 'Dy'), ('La', 'Ce', ' Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', 'Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', 'Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', 'Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', ' Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', 'Yb'), ('La', 'Pr', 'Lu'), ('La', 'Nd', 'Sm'), ('La', 'Nd', 'Eu'), ('La', 'Nd', 'Gd'), ('La', 'Nd', 'Tb'), ('La', 'Nd', 'Dy'), ('La', 'Nd', 'Ho'), ('La', 'Nd', 'Er'), ('La', 'Nd', 'Tm'), ('La', ' Nd', 'Yb'), ('La', 'Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), (' La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', 'Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', 'G d'), ('La', 'Eu', 'Tb'), ('La', 'Eu', 'Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', ' Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'G d', 'Tm'), ('La', 'Gd', 'Yb'), ('La', 'Gd', 'Lu'), ('La', 'Tb', 'Dy'), ('La', 'Tb', 'Ho'), ('La', 'Tb', 'Er'), ('La', 'Tb', 'Tm'), ('La', 'Tb', 'Yb'), ('La', 'Tb', 'Lu'), ('La', 'Dy', 'Ho'), ('La', 'Dy', 'Er'), ('La', 'Dy', 'Tm'), ('L a', 'Dy', 'Yb'), ('La', 'Dy', 'Lu'), ('La', 'Ho', 'Er'), ('La', 'Ho', 'Tm'), ('La', 'Ho', 'Yb'), ('La', 'Ho', 'Lu'), ('La', 'Er', 'Tm'), ('La', 'Er', 'Yb'), ('La', 'Er', 'Lu'), ('La', 'Tm', 'Yb'), ('La', 'Tm', 'Lu'), ('La', 'Yb', 'Lu' ), ('Ce', 'Pr', 'Nd'), ('Ce', 'Pr', 'Sm'), ('Ce', 'Pr', 'Eu'), ('Ce', 'Pr', 'Gd'), ('Ce', 'Pr', 'Tb'), ('Ce', 'Pr', 'Dy' ), ('Ce', 'Pr', 'Ho'), ('Ce', 'Pr', 'Er'), ('Ce', 'Pr', 'Tm'), ('Ce', 'Pr', 'Yb'), ('Ce', 'Pr', 'Lu'), ('Ce', 'Nd', 'Sm '), ('Ce', 'Nd', 'Eu'), ('Ce', 'Nd', 'Gd'), ('Ce', 'Nd', 'Tb'), ('Ce', 'Nd', 'Dy'), ('Ce', 'Nd', 'Ho'), ('Ce', 'Nd', 'Er'), ('Ce', 'Nd', 'Tm'), ('Ce', 'Nd', 'Yb'), ('Ce', 'Nd', 'Lu'), ('Ce', 'Sm', 'Eu'), ('Ce', 'Sm', 'Gd'), ('Ce', ' Sm', 'Tb'), ('Ce', 'Sm', 'Dy'), ('Ce', 'Sm', 'Ho'), ('Ce', 'Sm', 'Er'), ('Ce', 'Sm', 'Tm'), ('Ce', 'Sm', 'Yb'), ('Ce', 'Sm', 'Lu'), ('Ce', 'Eu', 'Gd'), ('Ce', 'Eu', 'Tb'), ('Ce', 'Eu', 'Dy'), ('Ce', 'Eu', 'Ho'), ('Ce', 'Eu', 'Er '), ('Ce', 'Eu', 'Tm'), ('Ce', 'Eu', 'Yb'), ('Ce', 'Eu', 'Lu'), ('Ce', 'Gd', 'Tb'), ('Ce', 'Gd', 'Dy'), ('Ce', 'Gd', 'Ho'), ('Ce', 'Gd', 'Er'), ('Ce', 'Gd', 'Tm'), ('Ce', 'Gd', 'Yb'), ('Ce', 'Gd', 'Lu'), ('Ce', 'Tb', 'Dy'), ('Ce', ' Tb', 'Ho'), ('Ce', 'Tb', 'Er'), ('Ce', 'Tb', 'Tm'), ('Ce', 'Tb', 'Yb'), ('Ce', 'Tb', 'Lu'), ('Ce', 'Dy', 'Ho'), ('C e', 'Dy', 'Er'), ('Ce', 'Dy', 'Tm'), ('Ce', 'Dy', 'Yb'), ('Ce', 'Dy', 'Lu'), ('Ce', 'Ho', 'Er'), ('Ce', 'Ho', 'Tm'), ('Ce', 'Ho', 'Yb'), ('Ce', 'Ho', 'Lu'), ('Ce', 'Er', 'Tm'), ('Ce', 'Er', 'Yb'), ('Ce', 'Er', 'Lu'), ('Ce', 'Tm', ' Yb'), ('Ce', 'Tm', 'Lu'), ('Ce', 'Yb', 'Lu'), ('Pr', 'Nd', 'Sm'), ('Pr', 'Nd', 'Eu'), ('Pr', 'Nd', 'Gd'), ('Pr', 'N d', 'Tb'), ('Pr', 'Nd', 'Dy'), ('Pr', 'Nd', 'Ho'), ('Pr', 'Nd', 'Er'), ('Pr', 'Nd', 'Tm'), ('Pr', 'Nd', 'Yb'), ('Pr', ' Nd', 'Lu'), ('Pr', 'Sm', 'Eu'), ('Pr', 'Sm', 'Gd'), ('Pr', 'Sm', 'Tb'), ('Pr', 'Sm', 'Dy'), ('Pr', 'Sm', 'Ho'), ('Pr ', 'Sm', 'Er'), ('Pr', 'Sm', 'Tm'), ('Pr', 'Sm', 'Yb'), ('Pr', 'Sm', 'Lu'), ('Pr', 'Eu', 'Gd'), ('Pr', 'Eu', 'Tb'), (' Pr', 'Eu', 'Dy'), ('Pr', 'Eu', 'Ho'), ('Pr', 'Eu', 'Er'), ('Pr', 'Eu', 'Tm'), ('Pr', 'Eu', 'Yb'), ('Pr', 'Eu', 'Lu'), (' Pr', 'Gd', 'Tb'), ('Pr', 'Gd', 'Dy'), ('Pr', 'Gd', 'Ho'), ('Pr', 'Gd', 'Er'), ('Pr', 'Gd', 'Tm'), ('Pr', 'Gd', 'Yb'), ('Pr', 'Gd', 'Lu'), ('Pr', 'Tb', 'Dy'), ('Pr', 'Tb', 'Ho'), ('Pr', 'Tb', 'Er'), ('Pr', 'Tb', 'Tm'), ('Pr', 'Tb', 'Yb'), ('Pr', 'Tb', 'Lu'), ('Pr', 'Dy', 'Ho'), ('Pr', 'Dy', 'Er'), ('Pr', 'Dy', 'Tm'), ('Pr', 'Dy', 'Yb'), ('Pr', 'Dy', 'Lu'), ('Pr', 'Ho', 'Er'), ('Pr', 'Ho', 'Tm'), ('Pr', 'Ho', 'Yb'), ('Pr', 'Ho', 'Lu'), ('Pr', 'Er', 'Tm'), ('Pr', 'Er', 'Yb'), ('Pr', 'Er', 'Lu'), ('Pr', 'Tm', 'Yb'), ('Pr', 'Tm', 'Lu'), ('Pr', 'Yb', 'Lu'), ('Nd', 'Sm', 'Eu'), ('Nd', 'Sm', 'Gd '), ('Nd', 'Sm', 'Tb'), ('Nd', 'Sm', 'Dy'), ('Nd', 'Sm', 'Ho'), ('Nd', 'Sm', 'Er'), ('Nd', 'Sm', 'Tm'), ('Nd', ' Sm', 'Yb'), ('Nd', 'Sm', 'Lu'), ('Nd', 'Eu', 'Gd'), ('Nd', 'Eu', 'Tb'), ('Nd', 'Eu', 'Dy'), ('Nd', 'Eu', 'Ho'), (' Nd', 'Eu', 'Er'), ('Nd', 'Eu', 'Tm'), ('Nd', 'Eu', 'Yb'), ('Nd', 'Eu', 'Lu'), ('Nd', 'Gd', 'Tb'), ('Nd', 'Gd', 'D y'), ('Nd', 'Gd', 'Ho'), ('Nd', 'Gd', 'Er'), ('Nd', 'Gd', 'Tm'), ('Nd', 'Gd', 'Yb'), ('Nd', 'Gd', 'Lu'), ('Nd', ' Tb', 'Dy'), ('Nd', 'Tb', 'Ho'), ('Nd', 'Tb', 'Er'), ('Nd', 'Tb', 'Tm'), ('Nd', 'Tb', 'Yb'), ('Nd', 'Tb', 'Lu'), (' Nd', 'Dy', 'Ho'), ('Nd', 'Dy', 'Er'), ('Nd', 'Dy', 'Tm'), ('Nd', 'Dy', 'Yb'), ('Nd', 'Dy', 'Lu'), ('Nd', 'Ho', ' Er'), ('Nd', 'Ho', 'Tm'), ('Nd', 'Ho', 'Yb'), ('Nd', 'Ho', 'Lu'), ('Nd', 'Er', 'Tm'), ('Nd', 'Er', 'Yb'), ('Nd', ' Er', 'Lu'), ('Nd', 'Tm', 'Yb'), ('Nd', 'Tm', 'Lu'), ('Nd', 'Yb', 'Lu'), ('Sm', 'Eu', 'Gd'), ('Sm', 'Eu', 'Tb'), ( 'Sm', 'Eu', 'Dy'), ('Sm', 'Eu', 'Ho'), ('Sm', 'Eu', 'Er'), ('Sm', 'Eu', 'Tm'), ('Sm', 'Eu', 'Yb'), ('Sm', 'Eu', ' Lu'), ('Sm', 'Gd', 'Tb'), ('Sm', 'Gd', 'Dy'), ('Sm', 'Gd', 'Ho'), ('Sm', 'Gd', 'Er'), ('Sm', 'Gd', 'Tm'), ('Sm ', 'Gd', 'Yb'), ('Sm', 'Gd', 'Lu'), ('Sm', 'Tb', 'Dy'), ('Sm', 'Tb', 'Ho'), ('Sm', 'Tb', 'Er'), ('Sm', 'Tb', 'Tm' ), ('Sm', 'Tb', 'Yb'), ('Sm', 'Tb', 'Lu'), ('Sm', 'Dy', 'Ho'), ('Sm', 'Dy', 'Er'), ('Sm', 'Dy', 'Tm'), ('Sm', 'D y', 'Yb'), ('Sm', 'Dy', 'Lu'), ('Sm', 'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', 'Yb'), ('Sm', 'Ho', 'Lu'), (' Sm', 'Er', 'Tm'), ('Sm', 'Er', 'Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', 'Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', 'Yb', ' Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', ' Gd', 'Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('E u', 'Tb', 'Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', 'Dy', 'Tm'), ('Eu', 'Dy', 'Yb'), ('Eu', 'Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', 'Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'T m'), ('Eu', 'Er', 'Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', 'Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', 'Yb', 'Lu'), ('Gd', 'Tb ', 'Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', 'Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', 'Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', 'Dy', 'Yb'), ('Gd', 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', 'Tm'), ('Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), ('Gd', 'Er', 'Tm'), ('Gd', 'Er', 'Yb'), ('Gd', 'Er', ' Lu'), ('Gd', 'Tm', 'Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', 'Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', ' Dy', 'Tm'), ('Tb', 'Dy', 'Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', 'Yb'), (' Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', 'Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', 'Yb'), ('Tb', 'Tm', 'Lu' ), ('Tb', 'Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', 'Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', 'Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', 'Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', 'Yb', 'Lu'), ('Ho', 'Er', 'Tm'), ('Ho', 'Er', 'Yb'), ('Ho', 'Er', 'Lu'), ('Ho', 'Tm', 'Yb'), ('Ho', 'Tm', 'Lu'), ('Ho', 'Yb', 'Lu'), (' Er', 'Tm', 'Yb'), ('Er', 'Tm', 'Lu'), ('Er', 'Yb', 'Lu'), ('Tm', 'Yb', 'Lu') 3. Example Verification methodology 3: this methodology expands on Verification methodology 2 by the use of naturally occurring microbial cation exchangers, including bacteria and fungi.i. As above but right before step vii (unsealing samples in laboratory), add the following steps:| ii. Lyse the microbes. For example, autoclave each sample-containing beaker for steam sterilization at 250 °F at 15 psi for 15 minutes. This may lyse any microbes and cause an active release of bio-adsorbed metals.| iii. Let sample-containing beakers cool to room temperature before proceeding.| iv. The filter in step (ix) may now act to additionally remove any larger aggregates of microbial cell suspensions that did not lyse in the autoclaving process.| v. The added EDTA in step (x) in Verification Methodology 2 may act to additionally chelate any REEs that are complexed to the cell wall or organic molecules of the microbial genetic material (as a result of cell lysis).| vi. In conjunction, verification methodology 3 provides a protocol to achieve full recovery of REEs that were retained in the top 10 cm of soil due to the following biogeochemical processes:1. Mineral surface interface complexation.| 2. The cation exchange capacity inherent to soils due to organic matter.| 3. Microbially mediated surface biosorption and/or active biological absorption pathways including but not limited to REE-aqueous complexation with internal genetic material of individual microbial cells found in natural soils and sediments. B. Example systems and methods to enhance the agronomic performance and ecosystem co-benefits:In these non-limiting embodiments, product formulations are detailed that improve the soil quality for improved agronomic applications as well as embodiments that specify improvements on crop health and an ability for plants to protect themselves from pathogens.| Addition of macronutrients that enhance the agronomic benefits of the applied mineral. Example: addition of elemental 1-5% by weight formulation K or Ca or inexpensive REE such as La to improve use cases of pulverized Mg2SiO4 by improving the nutrient balance of the soil to match the needs of actively growing plants. Application rates for K and Ca may range from 50-100 ppm and lanthanide addition rates may range from 1-50 ppm.| The 1-5% by volume addition of slow-release acidifiers in the form of elements that maintain the acidity of the soil despite the tendency of the applied mineral to reduce soil acidity in the weathering process. Example: addition of minerals with Al (such as gibbsite, Al(OH)3) or S (such as gypsum, CaSO4)-2H2O), in a rate of 1-10% by weight of total formulation, which contribute to maintaining soil acidity, and thus maintain high rates of weathering, which counteracts the tendency of forsterite weathering to increase alkalinity, which slows rates of weathering.| The incorporation of additional micronutrients such as zinc (1-5% by weight compared to mineral amendment) to reduce ecosystem losses of phosphorus and downstream ecosystem impacts of phosphate-based fertilizers, such as eutrophication. Phosphates are immobilized via precipitation reactions with the additional zinc metal, so zinc addition slows the transport and reduces mobility of phosphate in the subsoil. As a consequence, phosphate-based fertilizer applications can be performed more safely and with higher confidence that downstream waterways will not form algal blooms and lead to anoxic, uninhabitable waterways for aquatic life. The addition of 1-32 tons/hectare of mineral in conjunction with 1-5% by weight zinc in fields with heavy phosphate application reduces the likelihood of significant phosphate leaching. This also increases nutrient use efficiency, which reduces fertilizer cost to farmers and reduces negative environmental impacts to society. Specifically, phosphate-zinc precipitates become slow-releasing over time due to their immobilization in the soil as a solid phase. This provides longer timeframes for plants to access the phosphate application, reducing the frequency of fertilization.| The method of mixing of different mineral adjuvants to the primary mineral used for carbon removal can be varied, with impacts on performance. In some embodiments, the admixture (e.g., of gypsum and forsterite) could be completely emulsified. In some embodiments, a nutrient, such as urea, could represent a core that is subsequently coated with a shell of silicate mineral used for carbon removal. In some embodiments the silicate mineral could be the core, and the nutrient, such as urea, could be the coating. In each of these cases, the embodiment can be optimized so as to reduce environmental losses of the nutrient, and increase availability to the plant, while providing the acidity necessary for the silicate mineral weathering. In some embodiments, this may represent a "slow release" nutrient that does not mineralize too quickly and is synchronized more favorably with plant demand.| Comminution, or pulverization, may help reproduce the expected kinetics of alkalizers such as pulverized limestone or dolomite, known as aglime. Aglime has well-characterized kinetics originating in the particle size distribution of the product, which are in some jurisdictions legally regulated to meet certain requirements. A representative cross section of dissolution kinetics based on actual aglime mesh size observations is depicted in FIG. 2.|It naturally follows that agronomic performance expectations for silicate minerals used for ERW should follow similar reaction kinetics, particularly in the first year after application, while also meeting the goals for CDR. Thus, an ideal particle size distribution may be tuned to meet this goal. The following shows the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um, such as 90um, which closely approximates the alkalinity release dynamics for aglime.| The small particle sizes produced by pulverization as above are valuable for performance as an aglime substitute and CDR mechanism, but introduce their own set of potential challenges. One potential challenge is that small particle sizes may fall within regulated categories such as PM10 or PM2.5; another potential challenge is the product may not be easily transferred from one vessel to another (so-called "flowability") because it has a tendency to settle into a compact mass; the product may also not be applied uniformly by extant farm equipment; potentially low uniformity application impacts the agronomic performance as well as the sampling density needed for carbon removal verification. In one potential formulation, the product is pelletized after pulverization, using a common binder such as lignosulfate in a 3-5% ratio by weight of the total formulation. The amount of binder may be optimized to improve performance characteristics during transport and application, but minimize the water and energy needed to dissolve the pellet once it is in the field. Pelletizing the product, into a size range of, for example, 0.5 mm to 3 mm increases the flowability; reduces the prevalence of dust, including the risk of asbestos exposure; enables the use of extant crop input application equipment; and improves the evenness of field distribution, which has the agronomic and carbon verification benefits identified. Pelletizing in this size range also ensures that an adequate number of pellets fall onto any land area which may subsequently be sampled for analysis.| A desiccated but living biological compound, such as a mycorrhizal inoculum, may be used to coat the agglomerated and dried pellets, so as to enhance the dissolution of the pellet itself after application. This may be distinct from a fungal adjuvant to the pellet to increase dissolution of the silicate minerals themselves.| To accommodate a range of soil types from acidic to neutral pH, the product may be differentiated into different particle size distributions so as to achieve a consistent rate of weathering across different soil types. For example a consistent rate of weathering may be that the entire applied amount of mineral product weathers in 9 months, allowing a subsequent application every year. To achieve this, an acidic soil may have pellets that contain particles with a modal size on the order of 100 um, while a neutral soil may have pellets that contain particles with a modal size on the order of 10 um. The negative consequence of applying a fine particle in an acidic soil may be that it dissolves too quickly, swinging the pH of the soil too quickly, and altering the nutrient availability severely in the growing plant. The negative consequence of applying a coarse particle in a neutral soil may be that the particle weathers too slowly or is functionally inert, which does not remove carbon as intended, and may subject the farmer or the vendor to risk of clawbacks for payments received for carbon removal. C. Example systems and methods to control or enhance the performance as a securitized carbon removal method:In these non-limiting embodiments, product formulations are described that improve the marketability of pulverized and optionally pelletized mineral amendments as a verifiable carbon removal method, irrespective of their impact on agronomic performance. Such changes in marketability increase the value of the carbon product, for example for detecting and preventing fraud, or increase the dissolution rate (mass per area per year) to accelerate the timing of reapplication, which raises the value in a discounted cash flow analysis. The general scheme is depicted in FIG. 4.| The addition of low cost and inert trace elements, for example 1-5 ppm neodymium or lanthanum, to a mineral amendment, beyond the natural abundances present in the ore body, improves performance in Verification methods 2 and 3. Specifically, the additional elements reduce measurement uncertainty owing to low natural abundance calculations as well as uncertainty owing to variability from the source mineral. Reduction of these uncertainties improves the detectability of true positives and true negatives. This principle could be applied to many potential soil amendments and fertilizers to verify provenance as pertains to legal contracts.| The addition of binders to create aggregations of the ground mineral that could reduce drift, which improves distribution uniformity; reduces potential respiratory health impacts; and/or improves applicability of the applied mineral using commercially available equipment. For example, a biofilm mediating organic compound, such as alginate or chitosan, could be mixed with a pulverized mineral with a particle size of approximately 100 microns to achieve an aggregated pellet size of 1 millimeter. This would maintain the advantages of fine particle size, particularly the high specific surface area (m2/g) that mediates dissolution rate, while offsetting potential limitations outlined above. An example methodology for aggregating ground minerals could include these steps:∘ Dissolve 10 grams of alginate powder into solution to create a 0.5 M - 1.0 M alginic acid solution.| ∘ Heat solution to 80-100 °F to dissolve alginate powder fully if necessary.| ∘ Spray aerosol sized particles of dissolved alginate powder onto the ground rock material in order to create a biofilm-coated rock material. Apply a consistent spray of 100 mL for each 100 gram of rock (1:1 v/w).| ∘ The resulting aggregates may have increased bulk density as well as higher aggregating properties due to van der Waals force attraction between the individual rock particles. Dissolution rates can be modified by non-living organic molecules applied concurrently with the mineral amendment. For example, protonated microbes such as acid-treated Arthrobacter nicotianae can constitute an initial release of protons to attack the ground rock materials' crystal structure. This method of acidification for optimal accelerated weathering of rock material may occur even during winter/cold climate. Because biologically mediated processes can have sharp thresholds, e.g., under freezing conditions, such a chemically controlled process would exhibit greater ability to expedite rock breakdown over a range of environmental conditions. To implement this methodology, we outline the following steps:1) De-frost an aliquot of A. nicotianae in 5 mL of Luria broth for about 24 hours at exactly 30 °C.| 2) Sub-culture into a larger volume of Luria broth at a 1:50 dilution and allow growth for another 24 hours at 30 °C.| 3) During growth steps #1 and 2, cultures may be shaken, for example at 200-220 RPM, for aeration.| 4) After culture has been grown for 48 hours in total, centrifuge the cell suspension.| 5) Collect cell pellet and take a small amount and set it aside. Weigh wet weight, dry at 60 °C overnight, and weigh dry amount to obtain wet : dry conversion.| 6) Develop an OD600 to wet weight to dry weight conversion by taking 5 varying amounts of wet aliquots of wet biomass and measuring optical density given its known wet mass. Wet aliquots may have a mass of about 1, 4, 8, 12, 16 wet grams and be suspended in 100 mL of DI water.| 7) Wash cells in 0.1 M NaCl solution.a. Centrifuge cells+growth media at 4000xg.| b. Carefully pour out LB broth.| c. Add 0.1 M NaCl solution.| d. Centrifuge cells+NaCl solution at 4000xg.| e. Carefully pour out NaCl solution. 8) Protonate the cells while wet.a. Re-suspend the wet biomass in an acidic (e.g., pH 3.0) solution using a dilute hydrochloric acid solution (0.001-0.01 M).| b. Centrifuge cells+HCl solution at 4000xg.| c. Carefully pour out solution.| d. Repeat steps (a)-(c) a total of three times.| e. Dry cells in an oven at 80-100 °C for 48 hours.| f. Grind cells using a mortar/pestle to achieve a powder form. 9) Mix 5% w/w of dry cell powder with the ground rock material.| 10) When this particular rock material+cell powder mixture is applied to agricultural soils, the irrigation or rainfall will re-apply moisture and allow the pre-protonated, re-wet biomass to release their protons. This will ultimately induce a local acidity effect on the rock particle (molecular) level to accelerate rock crystal lattice breakdown. The cells act as biodegradable transporters that are also benign to the natural soil environment. Family Number|(103013820)|103013820|Abstract|(US11644454 B2)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.|(WO2022271842 A1)|La présente divulgation concerne des procédés de vérification d'une altération forcée améliorée à l'aide d'éléments de trace immobiles trouvés dans un amendement minéral. La divulgation concerne en outre des amendements minéraux qui permettent une altération forcée améliorée.|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.|(AU2022299180 A9)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.(From EP4276752 A3)|(CA3207124 A1)|La présente divulgation concerne des procédés de vérification d'une altération forcée améliorée à l'aide d'éléments de trace immobiles trouvés dans un amendement minéral. La divulgation concerne en outre des amendements minéraux qui permettent une altération forcée améliorée.|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.|(US11921098 B2)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.|(EP4256520 C0)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.|(EP4276752 A3)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.|(BR112023023226 B1)|verification methods and agronomic enhancements for carbon removal based on improved weathering of rocks. this description refers to methods to verify improved weathering of rocks using traces of immovable elements found within a mineral correction. mineral corrections that allow for improved weathering of rocks are also described|(US12422425 B2)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.|(US20260016458 A1)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.|CPC codes|(US11644454 B2)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(WO2022271842 A1)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(AU2022299180 A9)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(CA3207124 A1)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(US11921098 B2)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(EP4256520 C0)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(EP4276752 A3)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(BR112023023226 B1)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(US12422425 B2)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|(US20260016458 A1)|B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|G01N-033/24|IPC codes|(US11644454 B2)|G01N-033/24|(US11921098 B2)|G01N-033/24|(EP4256520 C0)|B01D-053/62|G01N-033/24|(EP4276752 A3)|B01D-053/34|B01D-053/62|G01N-033/24|(US12422425 B2)|G01N-033/24|(US20260016458 A1)|G01N-033/24|Title|(US11644454 B2)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(US20220404329 A1)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(WO2022271842 A1)|Procédés de vérification et améliorations agronomiques pour l'élimination de carbone sur la base d'une altération forcée améliorée|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(AU2022299180 A1)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(AU2022299180 A9)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(CA3207124 A1)|Procedes de verification et ameliorations agronomiques pour l'elimination de carbone sur la base d'une alteration forcee amelioree|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(US20230273174 A1)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(US11921098 B2)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(EP4256520 A1)|Procédés de vérification et améliorations agronomiques pour l'élimination de carbone sur la base d'une altération forcée améliorée|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(EP4256520 A4)|Procédés de vérification et améliorations agronomiques pour l'élimination de carbone sur la base d'une altération forcée améliorée|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(EP4256520 B1)|Procédés de vérification et améliorations agronomiques pour l'élimination de carbone sur la base d'une altération forcée améliorée|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(EP4256520 C0)|Procédés de vérification et améliorations agronomiques pour l'élimination de carbone sur la base d'une altération forcée améliorée|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(EP4276752 A2)|Procédés de vérification et améliorations agronomiques pour l'élimination de carbone sur la base d'une altération forcée améliorée|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(EP4276752 A3)|Procédés de vérification et améliorations agronomiques pour l'élimination de carbone sur la base d'une altération forcée améliorée|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(BR112023023226 A0)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(BR112023023226 A2)|Verification methods and agronomic improvements for carbon removal based on improved rock weathering|(BR112023023226 B1)|Method to verify enhanced rock weathering using a mineral correction|(US20240264139 A1)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(US12422425 B2)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(HK40094979 A)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(HK40095252 A)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering|(US20260016458 A1)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering| Analysis of biological materials|Basic materials chemistry|Computer technology|Electrical machinery, apparatus, energy|Environmental technology|Telecommunications B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|C09K-011/77|C09K-017/00|C09K-017/12|G01N-033/24|H01J-049/10/5|Y02C-020/40 B01D-053/62|B01D-2253/106|B01D-2253/304|B01D-2257/504|C09K-011/77|C09K-017/00|C09K-017/12|G01N-033/24|H01J-049/10/5|Y02C-020/40 B01D-053/34|B01D-053/62|C09K-011/77|C09K-017/00|C09K-017/12|G01N-033/24|G06T-007/00|G06T-007/60|G16C-020/20|G16C-020/70|H01J-049/10 B01D-053/34|B01D-053/62|C09K-011/77|C09K-017/00|C09K-017/12|G01N-033/24|G06T-007/00|G06T-007/60|G16C-020/20|G16C-020/70|H01J-049/10 WO2024156029|US20240383758|US12422425 WO2024156029 110849874 WHO=Examiner SELF=N CAT=X|US20240383758 112187058 WHO=Examiner SELF=N CAT=103|US12422425 103013820 WHO=Examiner SELF=Y US20210144935|US20210144935|US20210144935|JP07088362|US11921098|US20220065103|US20210144935|US20190086381|US20180082794|US6753957|US3864140|US3853573|US3856545 US20210144935 94130659 WHO=Examiner SELF=N CAT=A|US20210144935 94130659 WHO=Examiner SELF=N CAT=A|US20210144935 94130659 WHO=Examiner SELF=N CAT=A|JP07088362 24293047 WHO=Examiner SELF=N CAT=A|US11921098 103013820 WHO=Examiner SELF=Y|US20220065103 98850983 WHO=Examiner SELF=N|US20210144935 94130659 WHO=Applicant SELF=N|US20190086381 83774390 WHO=Examiner SELF=N|US20180082794 79099270 WHO=Examiner SELF=N|US6753957 43373580 WHO=Examiner SELF=N|US3864140 42244845 WHO=Examiner SELF=N|US3853573 42252986 WHO=Examiner SELF=N|US3856545 42260687 WHO=Examiner SELF=N |US11921098||US3853573; US3856545; US3864140|XP093021187; XP093021188; XP086574323; XP093021190; US20210144935|||US20210144935; XP086574323; XP093052931; XP093207104; XP085383712|US20210144935; XP086574323; JP07088362; XP055822446|||US6753957; US20180082794; US20190086381; US20220065103; US20210144935 (EP4256520)|Search Report references [Examiner]|-PAULO CARLOS ET AL: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), XP086574323, ISSN: 0883-2927, [retrieved on 20210406], DOI: 10.1016/J.APGEOCHEM.2021.104955|-MOOSDORF NILS ET AL: "Carbon Dioxide Efficiency of Terrestrial Enhanced Weathering", ENVIRONMENTAL SCIENCE &amp; TECHNOLOGY, vol. 48, no. 9, 8 April 2014 (2014-04-08), US, pages 4809 - 4816, XP093052931, ISSN: 0013-936X, DOI: 10.1021/es4052022|-LIU PU-LING ET AL: "Stable rare earth element tracers to evaluate soil erosion", SOIL AND TILLAGE RESEARCH, vol. 76, no. 2, 1 April 2004 (2004-04-01), NL, pages 147 - 155, XP093207104, ISSN: 0167-1987, DOI: 10.1016/j.still.2003.09.005|-See also references of WO 2022271842A1|-POTORT&#xfffd; ANGELA GIORGIA ET AL: "Traceability of Protected Geographical Indication (PGI) Interdonato lemon pulps by chemometric analysis of the mineral composition", JOURNAL OF FOOD COMPOSITION AND ANALYSIS, ELSEVIER, AMSTERDAM, NL, vol. 69, 15 March 2018 (2018-03-15), pages 122 - 128, XP085383712, ISSN: 0889-1575, DOI: 10.1016/J.JFCA.2018.03.001|-C. Paulo et al, Applied Geochemistry, 2021, 219, 104955|-N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809||(EP4276752)|Applicant references|-PAULO CARLOS ET AL: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), XP086574323, ISSN: 0883-2927, [retrieved on 20210406], DOI: 10.1016/J.APGEOCHEM.2021.104955|-SANNA A. ET AL: "A review of mineral carbonation technologies to sequester CO 2", CHEMICAL SOCIETY REVIEWS, vol. 43, no. 23, 1 January 2014 (2014-01-01), UK, pages 8049 - 8080, XP055822446, ISSN: 0306-0012, DOI: 10.1039/C4CS00035H||(US12422425)|Examiner references|||(US11644454)|Applicant references|-Haque et al. “Alkaline Mineral Soil Amendment: A Climate Change ‘Stabilization Wedge’?” Energies. 2019; 12 (12):2299. https://doi.org/10.3390/en12122299, Abstract; p. 8, para 2, 3.|-Haque et al. “Risk assessment of Nl, Cr, and Si release from alkaline minerals during enhanced weathering” Open Agriculture, vol. 5, No. 1, 2020, doi: https://doi.org/10.1515/opag-2020-0016, Abstract; p. 167 para 4-p. 168 para 1; p. 169, para 2.|-Paulo et al. “Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization.” Applied Geochemistry. Apr. 6, 2021, 129. 104955. 10.1016/j.apgeochem.2021. 104955. entire document.|-Strefler et al. (2018). “Potential and costs of carbon dioxide removal by enhanced weathering of rocks.” Environmental Research Letters. 13. 10.1088/1748-9326/aaa9c4. entire document.|-International Search Report and Written Opinion of the International Searching Authority for International Patent App. No. PCT/US22/34546 dated Nov. 15, 2022. (10 pages).|||(WO2022/271842)|International Search Report [Examiner]|-HAQUE FATIMA, CHIANG YI, SANTOS RAFAEL: "Alkaline Mineral Soil Amendment: A Climate Change ‘Stabilization Wedge’?", ENERGIES, vol. 12, no. 12, pages 2299, XP093021187, DOI: 10.3390/en12122299|-HAQUE FATIMA, CHIANG YI WAI, SANTOS RAFAEL M.: "Risk assessment of Ni, Cr, and Si release from alkaline minerals during enhanced weathering", OPEN AGRICULTURE, vol. 5, no. 1, 1 January 2020 (2020-01-01), pages 166 - 175, XP093021188, DOI: 10.1515/opag-2020-0016|-PAULO CARLOS; POWER IAN M.; STUBBS AMANDA R.; WANG BAOLIN; ZEYEN NINA; WILSON SIOBHAN A.: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), AMSTERDAM, NL , XP086574323, ISSN: 0883-2927, DOI: 10.1016/j.apgeochem.2021.104955|-GREGORY UPSCALING, NEMET F, CALLAGHAN MAX W, FELIX, STREFLER JESSICA, AMANN THORBEN, BAUER NICO, KRIEGLER ELMAR, HARTMANN JENS: " Potential and costs of carbon dioxide removal by enhanced weathering of rocks", ENVIRONMENTAL RESEARCH LETTERS, 1 January 2018 (2018-01-01), pages 34010, XP093021190, Retrieved from the Internet &lt;URL:https://iopscience.iop.org/article/10.1088/1748-9326/aaa9c4/pdf&gt; [retrieved on 20230206]|-See also references of EP 4256520A4|||||| GRANTED (EP4256520)|GRANTED|(EP4276752)|PENDING|(US12422425)|GRANTED|(US11921098)|GRANTED|(US11644454)|GRANTED|(US20260016458)|PENDING|(WO2022/271842)|LAPSED|(BR112023023226)|GRANTED|(AU2022299180)|PENDING|(HK40095252)|PENDING|(HK40094979)|PENDING|(CA3207124)|PENDING ALIVE (EP4256520)|ALIVE|(EP4276752)|ALIVE|(US12422425)|ALIVE|(US11921098)|ALIVE|(US11644454)|ALIVE|(US20260016458)|ALIVE|(WO2022/271842)|DEAD|(BR112023023226)|ALIVE|(AU2022299180)|ALIVE|(HK40095252)|ALIVE|(HK40094979)|ALIVE|(CA3207124)|ALIVE (EP4256520)|LEGAL DETAILS FOR EP4256520|Actual or expected expiration date=2042-06-22|Legal state=ALIVE|Status=GRANTED|Event 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CITY=Princeton , STATE=NJ , COUNTRY=US|(HK40094979)|NAME=Eion Corp 82 Spruce St., Princeton, New Jersey 08542 , COUNTRY=US|(US11921098)|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US , ATYP=US Company|(US20230273174)|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US|(WO2022/271842)|NAME=EION CORP. 82 Spruce St. Princeton, New Jersey 08542 , COUNTRY=US|(US11644454)|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US , ATYP=US Company|(US20220404329)|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US (EP4256520)|IT|(EP4256520)|IT|(EP4276752)|IT|(EP4276752)|IT||||(WO2022/271842)|US|(AU2022299180)|NZ|(AU2022299180)|NZ|(HK40095252)|HK|(HK40094979)|HK|(CA3207124)|CA (EP4256520)|NAME=Dragotti & Associati S.P.A. Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101869514|(EP4256520)|NAME=Pistolesi, Roberto;Dragotti & Associati Srl Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101195246|(EP4276752)|NAME=Dragotti & Associati S.R.L. Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101869514|(EP4276752)|NAME=Pistolesi, Roberto;Dragotti & Associati Srl Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101195246|(US12422425)|NAME=Frost Brown Todd LLP NAME=VanDrake, III Vance V. NAME=Johnson Alexander J.|(US11921098)|NAME=Frost Brown Todd LLP NAME=VanDrake, III Vance V. NAME=Johnson Alexander J.|(US11644454)|NAME=Ulmer & Berne LLP NAME=Van Drake, III Vance V. NAME=Johnson Alexander J.|(WO2022/271842)|NAME=FALK, Daniel T. et al. 1660 W. 2nd Street Suite 1100 Cleveland, Ohio 44113 , POSTCODE=44113 , COUNTRY=US|(AU2022299180)|NAME=AJ Pietras IP Limited Level 2, Bloomfield House 46/50 Bloomfield Terrace , CITY=Lower Hutt , STATE=Wellington , POSTCODE=5010 , COUNTRY=NZ|(AU2022299180)|NAME=AJ Pietras IP Limited Level 1, 29 Kings Crescent , CITY=Lower Hutt , STATE=Wellington , POSTCODE=5010 , COUNTRY=NZ|(HK40095252)|NAME=HNC INNOVATION LIMITED , COUNTRY=HK|(HK40094979)|NAME=HNC INNOVATION LIMITED , COUNTRY=HK|(CA3207124)|NAME=BURNET, DUCKWORTH & PALMER LLP , COUNTRY=CA |(EP4256520)|US; US; US||(EP4256520)|US; US; US|(EP4276752)|US; US; US|(EP4276752)|US; US; US|(US12422425)|US; US; US|(US20240264139)|US; US; US|(US11921098)|US; US; US|(US20230273174)|US; US; US|(US11644454)|US; US; US|(US20220404329)|US; US; US|(US20260016458)|US; US; US|(WO2022/271842)|US; US; US|||||||(CA3207124)|US; US; US (EP4256520)|NAME=WOLF, Adam|NAME=CHANG, Elliot Suk-Hyun|NAME=TANK, Alan Robert|(EP4256520)|NAME=WOLF, Adam, CITY=Princeton, New Jersey 08542, COUNTRY=US |NAME=CHANG, Elliot Suk-Hyun, CITY=Berkeley, California 94703, COUNTRY=US |NAME=TANK, Alan Robert, CITY=Bethesda, Maryland 20816, COUNTRY=US|(EP4256520)|NAME=WOLF, Adam|NAME=CHANG, Elliot Suk-Hyun|NAME=TANK, Alan Robert|(EP4256520)|NAME=WOLF, Adam, CITY=Princeton, New Jersey 08542, COUNTRY=US |NAME=CHANG, Elliot Suk-Hyun, CITY=Berkeley, California 94703, COUNTRY=US |NAME=TANK, Alan Robert, CITY=Bethesda, Maryland 20816, COUNTRY=US|(EP4276752)|NAME=WOLF, Adam, CITY=Princeton, 08542, COUNTRY=US |NAME=CHANG, Elliot Suk-Hyun, CITY=Foster City, 94404, COUNTRY=US |NAME=TANK, Alan Robert, CITY=Bethesda, 20816, COUNTRY=US|(EP4276752)|NAME=WOLF, Adam, CITY=Princeton, 08542, COUNTRY=US |NAME=CHANG, Elliot Suk-Hyun, CITY=Foster City, 94404, COUNTRY=US |NAME=TANK, Alan Robert, CITY=Bethesda, 20816, COUNTRY=US|(US12422425)|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US |NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US |NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US|(US20240264139)|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US |NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US |NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US|(US11921098)|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US |NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US |NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US|(US20230273174)|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US |NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US |NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US|(US11644454)|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US |NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US |NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US|(US20220404329)|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US |NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US |NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US|(US20260016458)|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US |NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US |NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US|(WO2022/271842)|NAME=WOLF, Adam 82 Spruce St. Princeton, New Jersey 08542, POSTCODE=08542, COUNTRY=US |NAME=CHANG, Elliot Suk-Hyun 1905 Grant Street Berkeley, California 94703, POSTCODE=94703, COUNTRY=US |NAME=TANK, Alan Robert 5324 Portsmouth Road Bethesda, Maryland 20816, POSTCODE=20816, COUNTRY=US|(BR112023023226)|NAME=WOLF ADAM|NAME=CHANG ELLIOT SUK-HYUN|NAME=TANK ALAN ROBERT|(BR112023023226)|NAME=WOLF ADAM|NAME=CHANG ELLIOT SUK-HYUN|NAME=TANK ALAN ROBERT|(AU2022299180)|NAME=WOLF, Adam|NAME=CHANG, Elliot Suk-Hyun|NAME=TANK, Alan Robert|(AU2022299180)|NAME=WOLF, Adam|NAME=CHANG, Elliot Suk-Hyun|NAME=TANK, Alan Robert|(HK40095252)|NAME=WOLF Adam|NAME=CHANG Elliot Suk-Hyun|NAME=TANK Alan Robert|(HK40094979)|NAME=WOLF Adam|NAME=CHANG Elliot Suk-Hyun|NAME=TANK Alan Robert|(CA3207124)|NAME=WOLF, ADAM, COUNTRY=US |NAME=CHANG, ELLIOT SUK-HYUN, COUNTRY=US |NAME=TANK, ALAN ROBERT, COUNTRY=US 39 7 Titre: (EP4256520)|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering Résumé: (EP4256520)|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering. 10 Abstract gpt-4o-mini yes The article discusses methods for verifying enhanced rock weathering and mentions mineral amendments that facilitate this process, which aligns with the goal of carbon removal through accelerated weathering.
13 CN202310125395 WOCN2024/075922|CN202310125395 WO2024/169718|CN116161660 105090822 WO2024/169718 A1 2024-08-22 [WO2024169718]|CN116161660 A 2023-05-26 [CN116161660] 2023-02-16 2024-02-05|2023-02-16 2024-08-22|2023-05-26 (WO2024/169718)|2026-08-16|(CN116161660)|2025-03-18 (WO2024/169718)|Technique for improving carbon sequestration potential of silicate minerals by means of sludge-cow dung mixed composting (WO2024/169718)|Disclosed in the present invention is a technique for improving the carbon sequestration potential of silicate minerals by means of sludge-cow dung mixed composting. The technique comprises: mixing residual sludge of a sewage plant with cow dung, adding a bulking agent and a conditioning agent for a composting treatment, adding a composite microbial agent of Bacillus mucilaginosus and Aspergillus niger when the temperature of the compost is reduced to a medium-temperature state from a high-temperature stage, adding a mycorrhizal inoculant to the decomposed compost product, then mixing same with silicate minerals in a mass ratio of (0.5-1.2):100, paving the resulting mixture into a shallow plate reactor, spraying with urban sewage, non-point source wastewater or diluted organic wastewater to keep the moisture of the mixed material layer at 35-55%, and introducing mixed gas containing CO2 for a carbon sequestration reaction. In the present invention, the compost product that is rich in organic matter and good for growth and reproduction of composite microorganisms is prepared, and the weathering of silicate minerals is accelerated and the carbon sequestration effect of the silicate minerals is improved, thus achieving multiple action effects of organic matter waste recycling, mining area ecological restoration and CO2 sequestration. KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY|UNIVERSITY KUNMING SCIENCE TECHNOLOGY (WO2024/169718)|KUNMING UNIVERSITY OF SCIENCE AND TECHNOLOGY ([CN])|(CN116161660)|KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) LIU SHUGEN|WANG QIONGHUI|TIAN SENLIN|SUN YI|PENG YUXIN|NING PING|LI YINGJIE (WO2024/169718)|LIU, Shugen|WANG, Qionghui|TIAN, Senlin|SUN, Yi|PENG, Yuxin|NING, Ping|LI, Yingjie (WO2024/169718)|BEIJING GAOWO LAW FIRM ([CN])|(CN116161660)|ZHANG YU;Kunming Tongju Patent Agency Co., Ltd.|Reg. Nb: 53214 (CN116161660)|The action process of biological weathering and carbon fixation of silicate minerals is limited by the structural characteristics of the minerals, and is also closely related to the growth and propagation and metabolism regulation and control of microorganisms, environmental influence factors such as organic matters, humidity, functional microorganism population structural characteristics and the like.|With the progress of human society in production and life, carbon dioxide (CO 2 ) Methane (CH) 4 ) Nitrous oxide (N) 2 O) the gas emission of the isothermal chamber is rapidly increased, and the greenhouse effect caused by the gas emission is responsible for a plurality of environmental problems such as glacier melting, sea level rising, extreme weather, forest fire and the like.| (WO2024/169718)|1. The invention relates to a method for improving the carbon-fixing potential of silicate minerals by a sludge-cow manure mixed compost, which is characterized in that the method comprises the following steps: S1, after the residual sludge of an urban sewage plant is mixed with cow manure, a bulking agent and a tempering agent are added into the obtained sludge-cow manure mixture to carry out composting treatment; S2, the temperature of a pile body falls back to near room temperature after the temperature of the pile body is increased and cooled, wherein, when the temperature of the pile body is reduced to 36 to 40°C after the temperature of the pile body is increased, the bulking agent and the tempering agent are added to carry out the composting treatment The composite microbial inoculant is added into the compost body and is subjected to continuous composting and fermentation treatment; after S3 and composting is finished, the mycorrhizal inoculant is added into the decomposed composting product obtained by S2, and then is evenly mixed with silicate minerals and is placed in a shallow flat plate reactor to keep the moisture and humidity, and the mixed gas containing CO2 is introduced for carbon fixation reaction.| (WO2024/169718)|Disclosed in the present invention is a technique for improving the carbon sequestration potential of silicate minerals by means of sludge-cow dung mixed composting.|The invention provides a technical method for improving the carbon-fixing potential of silicate minerals by sludge-cow manure mixed composting, which comprises the following steps: composting is carried out after mixing residual sludge, cow manure, crop straws and quenchants in a sewage plant according to a certain proportion; composite microbial inoculants are added into a compost body in a middle temperature state; mycorrhizal inoculants are added into composting products after being decomposed; after being uniformly mixed with silicate minerals, the composting products are laid in a flat reactor; organic small molecular acids are generated by the metabolism of composite microbial substrates to accelerate the weathering of the silicate minerals and further improve the carbon-fixing reaction process of the silicate minerals. In order to achieve the purpose, the invention provides a method for improving the carbon sequestration potential of silicate minerals by using sludge-cow manure mixed compost, which comprises the following steps:| (WO2024/169718)|SILICATE MINERAL(100,43)|MYCORRHIZAL INOCULANT(100,20)|SLUDGE COW DUNG(100,9)|SLUDGE COW MANURE(100,9)|CARBON SEQUESTRATION(100,8)|CARBON FIXING(100,3)|MIXED COMPOST(100,3)|SILICATE MINERAL POTENTIAL(100,1)|COMPOSITE MICROBIAL INOCULANT(59,2)|RESIDUAL SLUDGE(57,3)|PILE TEMPERATURE(54,4)|COMPOSITE MICROBIAL SUBSTRATE METABOLISM(47,1)|DECOMPOSED COMPOSTING PRODUCT(47,1)|COMPOSITE MICROBIAL INOCULUM(43,9)|COMPOSTING TREATMENT(42,9)|COMPOSITE MICROORGANISM REPRODUCTION(42,1)|BACILLUS MUCILAGINOSUS(41,6)|HIGHLAND BARLEY STRAW(41,2)|COMPOST(37,2)|CROP STRAW(37,1)|MICROBIAL INOCULANT(36,2)|ACCELERATE WEATHERING(35,2)|COMPOSITE MICROBIAL SUBSTRATE(35,1)|URBAN SEWAGE PLANT(34,2)|SEWAGE PLANT RESIDUAL SLUDGE(34,1)|COMPOSTING(33,7)|EXTRARHIZOSPHERE MYCELIUM(32,2)|TEMPERING(31,4)|COW MANURE(31,2)|DECOMPOSED COMPOST PRODUCT(30,1)|PUTREFIED COMPOST PRODUCT(30,1)|CALCIUM SILICATE TAILING(28,5)|ORGANIC WASTEWATER(28,3)|MIXED COMPOSTING(28,2)|MYCORRHIZAL FUNGUS SPORE(27,3)|FERMENTATION TREATMENT(27,2)|SEWAGE PLANT EXCESS SLUDGE(27,1)|SHALLOW PLATE REACTOR(26,8)|COMPOSTING PRODUCT(26,7)|SILICATE MINERAL WEATHERING(25,2)|CLOVER POT(23,3)|RHIZOSPHERE SOIL(23,3)|QUENCHER(23,2)|NONPOINT SOURCE WASTEWATER(21,3)|WHEAT STRAW(21,3)|FLAT REACTOR(21,1)|QUENCHANT(21,1)|COMPOST PRODUCTION(20,7)|SEWAGE PLANT(20,7)|BULKING AGENT(20,6)|CALCIUM FELDSPAR(20,5)|POTASSIUM FELDSPAR(20,4)|SHALLOW FLAT(20,2)|PEANUT SHELL(19,2)|ASPERGILLUS NIGER(17,6)|CO2 SEQUESTRATION(16,1)|MIDDLE TEMPERATURE(16,1)|COMPOSTING(15,2)|CO2(14,10)|SWELLING AGENT(14,2)|HUMIDITY(13,3)|RICE STRAW(13,3)|REACTING CARBON SEQUESTRATION(13,2)|VERSIORM(12,3)|ORGANIC MATTER WASTE RECYCLING(12,1)|CARBON FIXATION REACTION(11,9)|COLONY QUANTITY RATIO(11,5)|DRUM(11,3)|INFECTED ROOT SECTION(11,3)|CARBON FIXING REACTION(11,2)|SILICATE BACTERIUM METABOLISM(11,2)|CONDITIONING AGENT(11,1)|MIXED GAS(10,8)|REACTOR(10,7)|MIXTURE LAYER HUMIDITY(10,3)|MINING AREA ECOLOGICAL RESTORATION(10,2)|CARBON FIXATION(9,11)|CO2 VOLUME FRACTION(9,7)|CORN STRAW(9,3)|MOLECULAR ACID(9,1)|SLUDGE COW DUNG COMPOST(9,1)|GREENHOUSE PLANTING(8,2)|MIXED MICROBIAL INOCULUM(8,2)|SILICATE WEATHERING(8,2)|SILICATE ROCK WEATHERING(8,1)|UNUSED MINE TAILING(8,1)|BRAN(7,5)|SEWAGE PLANT REMAINING SLUDGE(7,3)|SHALLOW FLAT REACTOR(7,3)|FUNGUS COMPOSITE MICROBE(7,1)|FUNGUS COMPOSITE MICROORGANISM(7,1)|GRANULAR CORN STALK(7,1)|COMPOSTING FERMENTATION TREATMENT(6,1)|EXTRAROOT HYPHA(6,1)|FELDSPAR ORE POWDER(6,1)|MODIFIER(5,4)|RESOURCE UTILIZATION(5,2)|ROOM TEMPERATURE(5,2)|ALKALINE SILICATE(5,1)|DIATOM DIE(5,1)|FELDSPAR MINERAL(5,1)|ILLITE ORE(5,1)|MEDIUM TEMPERATURE(5,1)|MIXED MATERIAL LAYER MOISTURE(5,1)|MUNICIPAL SEWAGE(5,1)|ORGANIC SMALL MOLECULAR ACID(5,1)|POTASH FELDSPAR(5,1)|SILICATE MINERAL BIOWEATHERING(5,1)|SILICATE ROCK ENHANCED WEATHERING(5,1)|WOLLASTONITE MINERAL(5,1)|VOLUME MASS RATIO(4,3)|SLUDGE MIXING(4,2)|ATMOSPHERIC CO2 FIXATION(4,1)|CAPTURING ATMOSPHERIC CO2(4,1)|CARBONATE ROCK(4,1)|GLOBAL ATMOSPHERIC CO2(4,1)|MINERAL DISSOLUTION(4,1)|POTASSIUM SILICATE MINERAL POWDER(4,1)|PRODUCTION INTENSIFICATION(4,1)|RAPID SOIL UTILIZATION(4,1)|SOIL CIRCLE(4,1)|SUSTAINABLE DEVELOPMENT SOLUTION(4,1)|PARTICLE SIZE(3,6)|POTASSIUM BEARING SILICATE MINERAL(3,2)|RISING TEMPERATURE(3,2)|TRANSFORMATION(3,2)|WASTEWATER(3,2)|ABSORB CO2(3,1)|CROP GROWTH(3,1)|DRIED COMPOSTING PRODUCT(3,1)|INORGANIC POWDER(3,1)|MICROBIAL CARBON FIXATION(3,1)||(CN116161660)|SILICATE MINERAL(100,46)|CARBON FIXATION(100,28)|SLUDGE COW DUNG(100,19)|COMPOST(100,1)|MIXED COMPOST(100,1)|MYCORRHIZAL INOCULANT(70,16)|COMPOSTING FERMENTATION(50,1)|ADDING BACILLUS MUCILAGINOSUS(45,1)|COMPOSTING PRODUCT(43,5)|COMPOUND MICROBIAL INOCULANT(38,2)|DECOMPOSED COMPOSTING PRODUCT(36,1)|MUNICIPAL SEWAGE PLANT(34,1)|POTTED CLOVER PROPAGATION(34,1)|EXCESS SLUDGE(33,8)|ACCELERATE WEATHERING(33,1)|URBAN SEWAGE(31,5)|SEWAGE PLANT EXCESS SLUDGE(31,4)|HIGHLAND BARLEY STRAW(31,2)|DECOMPOSED COMPOST PRODUCT(30,4)|METABOLISM REGULATION(29,1)|COMPOUND MICROBIAL SUBSTRATE METABOLISM(28,1)|ORGANIC WASTEWATER(27,3)|MICROBIAL INOCULANT(27,2)|CROP STRAW(27,1)|MYCORRHIZA INOCULANT(27,1)|COMPOSTING TREATMENT(26,6)|FOREST FIRE(26,1)|GLACIER MELTING(26,1)|COMPOUND MICROORGANISM PROPAGATION(25,1)|KEEPING MOISTURE(25,1)|MOISTURE HUMIDITY(24,7)|ISOTHERMAL CHAMBER GAS EMISSION(24,1)|MICROORGANISM FUNCTION(24,1)|GAS EMISSION(23,2)|ISOTHERMAL CHAMBER(23,1)|SILICATE MINERAL WEATHERING(23,1)|PILE TEMPERATURE(22,4)|ORGANIC MICROMOLECULAR ACID(22,1)|CALCIUM SILICATE TAILING(21,5)|COMPOUND MICROBIAL SUBSTRATE(21,1)|COW DUNG(20,14)|MYCORRHIZAL FUNGUS SPORE(20,3)|NONPOINT SOURCE WASTEWATER(20,3)|PILE(19,8)|ASPERGILLUS NIGER(18,9)|SEWAGE PLANT(18,6)|HUMIDITY(18,2)|COMPOSTING(17,6)|INFECTED ROOT SEGMENT(17,3)|RHIZOSPHERE SOIL(17,3)|BULKING AGENT(16,8)|POTASSIUM FELDSPAR(16,4)|COMPOST PRODUCTION(15,9)|MICROORGANISM(15,4)|WHEAT STRAW(15,3)|MEDIUM TEMPERATURE(15,2)|SHALLOW FLAT REACTOR(15,1)|SHALLOW FLAT PLATE REACTOR(14,11)|CONDITIONING AGENT(14,9)|PEANUT SHELL(14,2)|MIXED MICROORGANISM(13,2)|SILICATE MINERAL CARBON FIXATION(13,2)|MIXED GAS(12,10)|METHANE(12,1)|ORGANIC MATTER RECYCLING(12,1)|CARBON SEQUESTRATION(11,2)|EXTREME WEATHER(11,1)|BIOLOGICAL WEATHERING(10,3)|ORGANIC MATTER(10,3)|PAVING THICKNESS(10,3)|HUMAN SOCIETY(10,1)|NITROUS OXIDE(10,1)|SEA LEVEL RISING(10,1)|PROPAGATION(9,3)|GLOMUSVERSIORM CLOVER BASINCULTIVATING(9,1)|COLONY QUANTITY RATIO(8,4)|NONPOINT SOURCE(8,3)|SILICATE BACTERIUM METABOLISM(8,2)|UNUTILIZED MINE TAILING(8,1)|CARBON FIXATION REACTION(7,6)|MINING AREA ECOLOGICAL RESTORATION(7,3)|STRAIN(7,2)|ADDING RATIO(7,1)|BACILLUS MUCILAGINOSUS BACTERIAL COLONY(7,1)|COMPOSITE MICROBIAL AGENT ACCOUNTING(6,2)|GREENHOUSE PLANTING(6,2)|CARBON FIXING(6,1)|MASS RATIO(5,10)|BRAN(5,5)|FLAT PLATE REACTOR(5,4)|MIXED MATERIAL LAYER(5,4)|CARBON DIOXIDE(5,2)|ADDING MYCORRHIZA INOCULANT(5,1)|CLOVER POTTED PLANT PROPAGATION(5,1)|COMPOSTING FERMENTATION TREATMENT(5,1)|FUNGUS COMPOSITE MICROORGANISM(5,1)|MIXTURERICE STRAW MASS(5,1)|SEA LEVEL(5,1)|WEIGHT RATIO(5,1)|INORGANIC POWDER(4,3)|GREENHOUSE EFFECT(4,2)|ANORTHITE MINERAL POWDER(4,1)|FELDSPAR MINERAL POWDER(4,1)|FUNGUS COMPOUND MICROORGANISM(4,1)|ILLITE MINERAL POWDER(4,1)|SEWAGE COW DUNG(4,1)|SEWAGE PLANT RESIDUAL SLUDGE(4,1)|BED(3,3)|VOLUME MASS RATIO(3,3)|MIXED COMPOSTING(3,2)|ACCELERATE SILICATE MINERAL(3,1)|DIATOM DIE(3,1)|DIATOM UTILIZATION(3,1)|GEOCHEMICAL CIRCULATION COURSE(3,1)|GRANULAR CORN STRAW(3,1)|MINERAL DISSOLUTION(3,1)|POTASSIUM SILICATE MINERAL POWDER(3,1)|POTASSIUM TRANSFORMATION(3,1)|SILICATE MINERAL BIOLOGICAL WEATHERING(3,1)|SILICATE MINERAL WEATHERATION(3,1)|URBAN SEWAGE PLANT(3,1)|WOLLASTONITE MINERAL(3,1)|CARRYING OUT CARBON FIXATION(2,5)|PARTICLE SIZE(2,5)|ADSORPTION(2,2)|CITRIC ACID PRODUCTION WASTEWATER(2,2)|SOURCE SEWAGE(2,2)|ADDING MIXED STRAW(2,1)|ATMOSPHERIC LOOP(2,1)|CROP GROWTH(2,1)|DRIED COMPOST PRODUCT(2,1)| (WO2024/169718)|1. The invention relates to a method for improving the carbon-fixing potential of silicate minerals by a sludge-cow manure mixed compost, which is characterized in that the method comprises the following steps: |S1, after the residual sludge of an urban sewage plant is mixed with cow manure, a bulking agent and a tempering agent are added into the obtained sludge-cow manure mixture to carry out composting treatment; |S2, the temperature of a pile body falls back to near room temperature after the temperature of the pile body is increased and cooled, wherein, when the temperature of the pile body is reduced to 36 to 40°C after the temperature of the pile body is increased, the bulking agent and the tempering agent are added to carry out the composting treatment The composite microbial inoculant is added into the compost body and is subjected to continuous composting and fermentation treatment; after |S3 and composting is finished, the mycorrhizal inoculant is added into the decomposed composting product obtained by S2, and then is evenly mixed with silicate minerals and is placed in a shallow flat plate reactor to keep the moisture and humidity, and the mixed gas containing CO2 is introduced for carbon fixation reaction.|2. According to the method described in Claim 1, the invention is characterized in that the ratio of the excess sludge of the sewage plant to the cow dung is (2-3):1.|3. The method according to Claim 1 is characterized in that the swelling agent is any one or more of rice straw, wheat straw, highland barley straw, peanut shell and corn straw; the addition amount of the swelling agent is 4% to 8% of the mass of the sludge-cow manure mixture.|4. According to the method in Claim 1, the invention is characterized in that the quencher is potassium feldspar and/or calcium feldspar; the addition amount of the quencher is 0.5% to 1.2% of the mass of the sludge-cow manure mixture.|5. According to the method in Claim 1, the method is characterized in that the composite microbial inoculum comprises Bacillus mucilaginosus and Aspergillus niger, the effective colony quantity ratio of the two is 1: (5-8), the two types of microorganisms are mixed and absorbed evenly with bran according to the volume mass ratio of 1: 10, and the composite microbial inoculum is added according to 0.8% to 1.5% of the mass of the bulk mixture.|6. According to the method described in claim 1, the method is characterized in that mycorrhizal inoculant is added to the putrefied compost product, and then mixed with silicate mineral according to (0.5-1.2):100; the silicate mineral is crushed to a particle size of 200 μm-5 mm.|7. According to the method in Claim 6, the invention is characterized in that the mycorrhizal inoculant and compost product are evenly mixed according to the proportion of (2-5):100; the preparation method of the mycorrhizal inoculant is that: the strain Glomus is prepared mosseae and Glomus The versiorm is propagated in a pot of clover in advance, and the mycorrhizal inoculant containing mycorrhizal fungi spores, extra-rhizosphere mycelium, infected root sections and rhizosphere soil is prepared.|8. According to the method in Claim 6, the silicate mineral is characterized in that the silicate mineral is a combination of calcium-based silicate tailings and any one of feldspar, illite and wollastonite in a mass ratio of 1:(2 to 5).|9. According to the method in Claim 1, the method is characterized in that compost products added with mycorrhizal inoculant are mixed with silicate minerals and then are laid flat to a shallow plate reactor, and the thickness of the lay-up is 1.0cm to 3.0cm.|10. According to the method as described in Claim 1 or 9, the method is characterized in that urban sewage, non-point source waste water or diluted organic waste water are sprayed to a shallow plate reactor, and the moisture and humidity of a mixture layer are kept at 35% to 55%.|11. According to the method described in claim 1, the composting process is characterized in that the equipment used for the composting process is a drum-type device; the composting process time is 15 days.|12. According to the method described in claim 1, the method is characterized in that the volume fraction of CO2 in the CO2 containing mixed gas is 0.04% to 0.05%. (WO2024/169718)|[0001] The Patent Office of the People's Republic of China (hereinafter referred to as the "Patent Office of the People's Republic of China"), Application No. CN202310125395.7, and Chinese patent application entitled "A Technical Method for Improving the Carbon Sequestration Potential of Silicate Minerals by Using Sludge-Cow Dung Compost" submitted on February 16, 2023 are required to have priority, and the entire contents of which are incorporated by reference in the present application.|technical field|[0002] The invention belongs to the technical field of microbial carbon fixation, in particular to a technical method for improving the carbon fixation potential of silicate minerals by sludge-cow manure mixed compost.|background technology|[0003] With the intensification of the production and living process of human society, the emission of carbon dioxide (CO2), methane (CH4), nitrous oxide (N2O) and other greenhouse gases increases rapidly. The greenhouse effect caused by the greenhouse effect causes glaciers to melt, sea level rise, extreme weather, forest fires and many other environmental problems. Therefore, CCUS (Carbon Capture, Utilization and Sequestration) technology has attracted much attention. During the geochemical cycle, the atmospheric CO2 transforms to HCO3-and most of them will eventually be deposited into carbonate rocks in the ocean, so as to regulate the content of atmospheric CO2 and the Earth's climate change, but this weathering regulation process is very slow. Enhanced weathering of silicate rocks is a negative emission technology based on geochemical principles. The technology accelerates the weathering of silicate rocks by adding silicate powder to farmland or forest, achieving more atmospheric CO2 fixation in a shorter period of time. Basalts are abundant and widely distributed in China, and there are a large number of unused mine tailings and alkaline silicate waste. It has great potential to remove atmospheric CO2 by enhancing the weathering of silicate rock.|[0004] There are many kinds of microorganisms in the surface environment, and the types of ecology and metabolism are various. Microbial activities can promote mineral dissolution, precipitation and transformation, thereby accelerating rock weathering, soil formation and the biogeochemical cycle of elements, changing the material composition of the soil circle, hydrosphere and atmosphere. The application of organic fertilizer containing potassium silicate mineral powder in soil improvement, crop growth and increasing soil carbon sink has been demonstrated, which provides a new idea for capturing atmospheric CO2 by the bioweathering of silicate mineral. In the face of the increasing of global atmospheric CO2 concentration and the greenhouse effect caused by it, it is of great significance to study and utilize the carbon sink effect caused by the weathering of silicate minerals for solving the current sustainable development and coping with global climate change. The prior patent CN202210246312.5 publishes a method for weathering silicate materials into soil and resource utilization, which utilizes silicate bacteria to promote the weathering of silicate-containing materials, releases potassium, phosphorus and other elements for absorption and utilization by diatom, the diatom grows to absorb CO2 in the air, and after the diatom dies, the diatom is mixed with the weathering materials to form the soil, thereby realizing rapid soil utilization of silicate solid waste at the same time of increasing carbon sink.|[0005] Most of the previous studies on the transformation of potassium-bearing silicate minerals by microorganisms were focused on silicate bacteria, but some studies showed that filamentous fungi had better weathering effect on potassium-bearing silicate minerals than bacteria. The process of weathering and carbon sequestration of silicate minerals is restricted by the structural characteristics of the minerals themselves, and is also closely related to the growth, reproduction and metabolic regulation of microorganisms, environmental impact factors such as organic matter, humidity and functional microbial population structure characteristics. The composting product with rich dissolved organic matter is prepared through mixing sludge and cow dung, and has the effects of promoting the growth, propagation and metabolism of silicate bacteria and fungi composite microbe, accelerating the weathering and carbon fixing reaction process of silicate minerals, and multiple functions of organic waste fixation, ecological restoration of mining area and CO2 fixation.|[0006] Contents of Invention|[0007] The invention provides a technical method for improving the carbon-fixing potential of silicate minerals by sludge-cow manure mixed composting, which comprises the following steps: composting is carried out after mixing residual sludge, cow manure, crop straws and quenchants in a sewage plant according to a certain proportion; composite microbial inoculants are added into a compost body in a middle temperature state; mycorrhizal inoculants are added into composting products after being decomposed; after being uniformly mixed with silicate minerals, the composting products are laid in a flat reactor; organic small molecular acids are generated by the metabolism of composite microbial substrates to accelerate the weathering of the silicate minerals and further improve the carbon-fixing reaction process of the silicate minerals.|[0008] In order to achieve the purpose, the invention provides a method for improving the carbon sequestration potential of silicate minerals by using sludge-cow manure mixed compost, which comprises the following steps:|[0009] S1. After mixing the excess sludge of the urban sewage plant with cow dung, adding bulking agent and tempering agent to the sludge-cow dung mixture for composting treatment;|[0010] S2, the temperature of the reactor dropped to near room temperature after the temperature rising and cooling stage, and when the temperature dropped to 36~40°C after the temperature rising, the composite microbial inoculum was added to the reactor and the continuous composting fermentation treatment was carried out.|[0011] After the composting is finished, mycorrhizal inoculant is added into the composting product obtained by S2, and then is evenly mixed with silicate minerals and is placed in a shallow plate reactor to keep moisture and humidity, and a mixed gas containing CO2 is introduced for carbon fixation reaction.|[0012] Further, the ratio of the excess sludge and the cow dung in the sewage plant is (2-3):1.|[0013] Furthermore, the bulking agent is any one or more of rice straw, wheat straw, highland barley straw, peanut shell and corn straw; the addition amount of the bulking agent is 4% to 8% of the mass of the mixture.|[0014] Furthermore, the modifier is potassium feldspar and/or calcium feldspar; preferably, the modifier consists of potassium feldspar and calcium feldspar in the mass ratio (2 to 4):1; the addition amount of the modifier is 0.5% to 1.2% of the mass of the sludge-cow manure mixture, and preferably, the addition amount of the modifier is 0.8% to 1.2% of the mass of the sludge-cow manure mixture.|[0015] Further, the composite microbial inoculum comprises Bacillus mucilaginosus and Aspergillus niger, the effective colony quantity ratio of the two is 1:(5-8), the two types of microorganisms are mixed and absorbed evenly with bran according to the volume-mass ratio of 1:10, the composite microbial inoculum is added according to 0.8% to 1.5% of the mass of the pile, and the preferred composite microbial inoculum is added according to 1.0% to 1.2% of the mass of the pile.|[0016] Further, mycorrhizal inoculant is added to the compost product which is putrescence, and then mixed with silicate mineral according to (0.5-1.2):100, preferably, and mixed with silicate mineral according to (0.8-1.0):100; the silicate mineral is crushed to a particle size of 200 μm-5mm, and preferably, the silicate mineral is crushed to a particle size of 600 μm-3mm.|[0017] Furthermore, the mycorrhizal inoculant and the compost product are evenly mixed according to the proportion of (2-5):100, and preferably, the mycorrhizal inoculant and the compost product are evenly mixed according to the proportion of (4-5):100; the preparation method of the mycorrhizal inoculant is that: the strain Glomus is prepared mosseae and Glomus The versiorm is propagated in a pot of clover in advance, and the mycorrhizal inoculant containing mycorrhizal fungi spores, extra-rhizosphere mycelium, infected root sections and rhizosphere soil is prepared.|[0018] Further, the silicate mineral is a combination of the calcium-based silicate tailings and any of feldspar, illite and wollastonite according to a mass ratio of 1:(2-5), and preferably, according to a mass ratio of 1:(4-5).|[0019] Furthermore, the compost product added with the mycorrhizal inoculant is mixed with silicate minerals and then is laid flat to a shallow plate reactor, and the layer thickness is 1.0cm to 3.0cm, and preferably, the layer thickness is 2.0 to 3.0cm.|[0020] Furthermore, urban sewage, non-point source wastewater or diluted organic wastewater are sprayed to the shallow flat reactor, and the humidity of the mixture layer is kept at 35% to 55%, and preferably, the humidity of the mixture layer is kept at 40% to 50%.|[0021] Further, the equipment used for the composting treatment is a drum-type device; the time for the composting treatment is 15 days; the invention utilizes the drum-type device to carry out the composting treatment according to the prior art.|[0022] Further, the volume fraction of CO2 in the CO2 containing mixed gas is 0.04% to 0.05%, and the invention is introduced with the mixed gas containing 0.04% to 0.05%CO2 to carry out carbon fixation reaction.|[0023] Compared with the prior art, the invention has the following technical effects:|[0024] (1) The invention utilizes the compost products with rich microbial population structure to accelerate the weathering of silicate minerals and improve the carbon fixing effect thereof, thereby realizing the multiple effect effects of organic waste fixation and resource utilization, ecological restoration in mining areas and CO2 fixation, and having good economic, environmental and social benefits.|[0025] (2) The invention adjusts the C/N ratio of the composting system by mixing sludge and cow dung, and adds bulking agent and tempering agent to carry out mixed composting; the obtained product contains dissolved organic substances such as protein, saccharide, hydrophilic organic acid and the like, and is beneficial to the growth, propagation and metabolism of silicate bacteria and fungi composite microorganisms, and accelerates the process of weathering and carbon fixation reaction of silicate minerals.|Specific Implementation Methods|[0026] The invention is further illustrated in the following specific embodiments, with detailed embodiments and operating procedures, but the scope of protection of the invention is not limited to the content.|[0027] Example 1|[0028] (1) The remaining sludge of the sewage plant and cow dung are mixed according to a ratio of 3:1, and granular corn stalks which are crushed to nearly 1cm are added according to a ratio of 6% of the mass of the obtained sludge-cow dung mixture; meanwhile, 75μm potash feldspar ore powder is added according to a ratio of 1.0% of the mass of the sludge-cow dung mixture; after fully mixed, dried composting products are added to adjust the initial water content of the composting mixture to 65%; and then a roller-type device is adopted to carry out composting treatment according to the prior art for 15d.|[0029] (2) The reactor is transferred to the cooling stage after the temperature rises to high temperature. When the temperature of the reactor is reduced to 36~40°C, a composite microbial inoculum with mass of 1.0% is added. The inoculum comprises Bacillus mucilaginosus and Aspergillus niger. The effective colony quantity ratio of the two inoculums is 1:6. After mixing, the inoculum is adsorbed evenly with bran according to the volume-mass ratio of 1:10. Then the inoculum is added into the reactor.|[0030] (3) After composting, the mycorrhizal inoculant was added into the composting product according to the mass ratio of 5:100. The preparation of mycorrhizal inoculant was as follows:The strain Glomus was selected as strain mosseae and Glomus The versiorm is cultivated in a clover pot, and the mycorrhizal inoculant containing mycorrhizal fungi spores, extra-root hypha, infected root sections and rhizosphere soil is prepared.|[0031] (4) The mixture of step (3) and the silicate mineral with a particle size of 600 μm are uniformly mixed according to a ratio of 1:100, and the silicate mineral consists of calcium-based silicate tailings and feldspar minerals according to a mass ratio of 1:2.|[0032] (5) The mixed materials obtained in step (4) are laid flat to a shallow flat reactor to form a material layer with a height of 2 cm. Urban sewage is periodically sprayed to maintain the moisture and humidity of the material layer at 40%, and CO2 volume fraction 0.05% mixed gas is introduced for carbon sequestration reaction.|[0033] The control group was set up, and the silicate minerals were directly laid out to the shallow flat reactor according to the step (4) to form a 2 cm height material layer. The municipal sewage was used to spray the water humidity of the material layer at 40% regularly, and the mixed gas of CO2 with the same concentration was introduced into the test group to carry out carbon fixation reaction. The concentration of CO2 in the gas phase at the upper part of the material layer was monitored in a sealed plate reactor. After 12h, the concentration of CO2 in the upper gas phase of the plate reactor decreased by 22.6% in the test group, while the decrease value of the control group was only 0.5%.|[0034] Example 2|[0035] (1) The remaining sludge of the sewage plant and the cow dung are mixed according to a ratio of 2:1, and rice straw with a length of about 1.5cm is added according to a ratio of 4% of the mass of the obtained sludge-cow dung mixture, and at the same time, calcium feldspar ore powder is added according to a ratio of 1.2% of the mass of the sludge-cow dung mixture, and composting treatment is carried out according to the prior art.|[0036] (2) When the reactor temperature is reduced to 38°C, a composite microbial inoculum of 1.3% mass of the reactor mixture is added, the effective colony quantity ratio of Bacillus mucilaginosus and Aspergillus niger is 1:8, and the mixed microbial inoculum is mixed with bran and absorbed evenly, and then added into the reactor.|[0037] (3) After composting, the mycorrhizal inoculant was added into the composting product according to the mass ratio of 2:100.|[0038] (4) The mixture of step (3) is uniformly mixed with silicate minerals with a particle size of 3mm according to a ratio of 1.2:100, and the silicate minerals consist of calcium-based silicate tailings and wollastonite minerals according to a mass ratio of 1:5.|[0039] (5) The mixed materials obtained in step (4) are laid flat to a shallow plate reactor to form a material layer with a height of 3 cm. The surface source sewage of greenhouse planting is periodically sprayed to keep the moisture and humidity of the material layer to be 55%, and the mixed gas with 0.04% of the volume fraction of CO2 is introduced to carry out the carbon fixation reaction.|[0040] A control group is arranged, and silicate minerals are directly laid on a shallow flat plate reactor according to step (4) to form a material layer with a height of 3cm; the surface source sewage of greenhouse planting is periodically sprayed to keep the water humidity of the material layer to be 55%; and the mixed gas with 0.04% of the volume fraction of CO2 is introduced to carry out the carbon fixation reaction. The remaining operations were the same as in Example 1. After 12h, the concentration of CO2 in the upper gas phase of the plate reactor decreased by 21.3% in the test group, but only 0.6% in the control group.|[0041] Example 3|[0042] (1) The remaining sludge of the sewage plant is mixed with the cow dung, mixed straws (wheat straws are mixed with corn straws in a ratio of 8% by weight of the obtained sludge-cow dung mixture) are added, feldspar ore powder (potassium feldspar ore powder is mixed with calcium feldspar ore powder in a ratio of 0.8% by weight of the sludge-cow dung mixture) is added, and compost treatment is carried out according to the prior art.|[0043] (2) When the reactor temperature is reduced to 38°C, a composite microbial inoculum of 0.8% mass of the reactor mixture is added, the effective colony quantity ratio of the bacillus mucilaginosus and the aspergillus niger is 1:6, and the mixed microbial inoculum is evenly mixed with bran for adsorption, and then added into the reactor.|[0044] (3) After composting, the mycorrhizal inoculant was added into the composting product according to the mass ratio of 4:100.|[0045] (4) The mixture of step (3) and the silicate mineral with the particle size of 1.5mm are uniformly mixed according to the proportion of 0.8:100, and the silicate mineral consists of the calcium-based silicate tailings and illite ore powder according to the proportion of 1:4 by mass.|[0046] (5) The mixed materials obtained in step (4) are laid flat to a shallow plate reactor to form a material layer with a height of 1.5cm. The waste water from citric acid production is diluted to a chemical oxygen demand of 400mg/L and then periodically sprayed to keep the moisture and humidity of the material layer at 35%, and the mixed gas with 0.04% of the volume fraction of CO2 is introduced to carry out carbon fixation reaction.|[0047] A control group was set up, and silicate minerals were directly laid out to a shallow plate reactor according to step (4) to form a material layer with a height of 1.5cm. The wastewater from citric acid production was diluted to a chemical oxygen demand of 400mg/L and then sprayed regularly to keep the moisture of the material layer at 35%, and the mixed gas with 0.04% CO2 volume fraction was introduced to conduct carbon fixation reaction. The remaining operations were the same as in Example 1. After 12h, the concentration of CO2 in the upper gas phase of the plate reactor decreased by 26.2% in the test group, but only 0.3% in the control group.|[0048] In spite of that exhaustive description of the present invention, the above embodiment are only some but not all embodiments of the present invention, and other embodiments may be obtain without being creative according to the present embodiment, which are all within the scope of the present invention. (WO2024/169718)|[0001] The Patent Office of the People's Republic of China (hereinafter referred to as the "Patent Office of the People's Republic of China"), Application No. CN202310125395.7, and Chinese patent application entitled "A Technical Method for Improving the Carbon Sequestration Potential of Silicate Minerals by Using Sludge-Cow Dung Compost" submitted on February 16, 2023 are required to have priority, and the entire contents of which are incorporated by reference in the present application.|technical field|[0002] The invention belongs to the technical field of microbial carbon fixation, in particular to a technical method for improving the carbon fixation potential of silicate minerals by sludge-cow manure mixed compost.|background technology|[0003] With the intensification of the production and living process of human society, the emission of carbon dioxide (CO2), methane (CH4), nitrous oxide (N2O) and other greenhouse gases increases rapidly. The greenhouse effect caused by the greenhouse effect causes glaciers to melt, sea level rise, extreme weather, forest fires and many other environmental problems. Therefore, CCUS (Carbon Capture, Utilization and Sequestration) technology has attracted much attention. During the geochemical cycle, the atmospheric CO2 transforms to HCO3-and most of them will eventually be deposited into carbonate rocks in the ocean, so as to regulate the content of atmospheric CO2 and the Earth's climate change, but this weathering regulation process is very slow. Enhanced weathering of silicate rocks is a negative emission technology based on geochemical principles. The technology accelerates the weathering of silicate rocks by adding silicate powder to farmland or forest, achieving more atmospheric CO2 fixation in a shorter period of time. Basalts are abundant and widely distributed in China, and there are a large number of unused mine tailings and alkaline silicate waste. It has great potential to remove atmospheric CO2 by enhancing the weathering of silicate rock.|[0004] There are many kinds of microorganisms in the surface environment, and the types of ecology and metabolism are various. Microbial activities can promote mineral dissolution, precipitation and transformation, thereby accelerating rock weathering, soil formation and the biogeochemical cycle of elements, changing the material composition of the soil circle, hydrosphere and atmosphere. The application of organic fertilizer containing potassium silicate mineral powder in soil improvement, crop growth and increasing soil carbon sink has been demonstrated, which provides a new idea for capturing atmospheric CO2 by the bioweathering of silicate mineral. In the face of the increasing of global atmospheric CO2 concentration and the greenhouse effect caused by it, it is of great significance to study and utilize the carbon sink effect caused by the weathering of silicate minerals for solving the current sustainable development and coping with global climate change. The prior patent CN202210246312.5 publishes a method for weathering silicate materials into soil and resource utilization, which utilizes silicate bacteria to promote the weathering of silicate-containing materials, releases potassium, phosphorus and other elements for absorption and utilization by diatom, the diatom grows to absorb CO2 in the air, and after the diatom dies, the diatom is mixed with the weathering materials to form the soil, thereby realizing rapid soil utilization of silicate solid waste at the same time of increasing carbon sink.|[0005] Most of the previous studies on the transformation of potassium-bearing silicate minerals by microorganisms were focused on silicate bacteria, but some studies showed that filamentous fungi had better weathering effect on potassium-bearing silicate minerals than bacteria. The process of weathering and carbon sequestration of silicate minerals is restricted by the structural characteristics of the minerals themselves, and is also closely related to the growth, reproduction and metabolic regulation of microorganisms, environmental impact factors such as organic matter, humidity and functional microbial population structure characteristics. The composting product with rich dissolved organic matter is prepared through mixing sludge and cow dung, and has the effects of promoting the growth, propagation and metabolism of silicate bacteria and fungi composite microbe, accelerating the weathering and carbon fixing reaction process of silicate minerals, and multiple functions of organic waste fixation, ecological restoration of mining area and CO2 fixation.|[0006] Contents of Invention|[0007] The invention provides a technical method for improving the carbon-fixing potential of silicate minerals by sludge-cow manure mixed composting, which comprises the following steps: composting is carried out after mixing residual sludge, cow manure, crop straws and quenchants in a sewage plant according to a certain proportion; composite microbial inoculants are added into a compost body in a middle temperature state; mycorrhizal inoculants are added into composting products after being decomposed; after being uniformly mixed with silicate minerals, the composting products are laid in a flat reactor; organic small molecular acids are generated by the metabolism of composite microbial substrates to accelerate the weathering of the silicate minerals and further improve the carbon-fixing reaction process of the silicate minerals.|[0008] In order to achieve the purpose, the invention provides a method for improving the carbon sequestration potential of silicate minerals by using sludge-cow manure mixed compost, which comprises the following steps:|[0009] S1. After mixing the excess sludge of the urban sewage plant with cow dung, adding bulking agent and tempering agent to the sludge-cow dung mixture for composting treatment;|[0010] S2, the temperature of the reactor dropped to near room temperature after the temperature rising and cooling stage, and when the temperature dropped to 36~40°C after the temperature rising, the composite microbial inoculum was added to the reactor and the continuous composting fermentation treatment was carried out.|[0011] After the composting is finished, mycorrhizal inoculant is added into the composting product obtained by S2, and then is evenly mixed with silicate minerals and is placed in a shallow plate reactor to keep moisture and humidity, and a mixed gas containing CO2 is introduced for carbon fixation reaction.|[0012] Further, the ratio of the excess sludge and the cow dung in the sewage plant is (2-3):1.|[0013] Furthermore, the bulking agent is any one or more of rice straw, wheat straw, highland barley straw, peanut shell and corn straw; the addition amount of the bulking agent is 4% to 8% of the mass of the mixture.|[0014] Furthermore, the modifier is potassium feldspar and/or calcium feldspar; preferably, the modifier consists of potassium feldspar and calcium feldspar in the mass ratio (2 to 4):1; the addition amount of the modifier is 0.5% to 1.2% of the mass of the sludge-cow manure mixture, and preferably, the addition amount of the modifier is 0.8% to 1.2% of the mass of the sludge-cow manure mixture.|[0015] Further, the composite microbial inoculum comprises Bacillus mucilaginosus and Aspergillus niger, the effective colony quantity ratio of the two is 1:(5-8), the two types of microorganisms are mixed and absorbed evenly with bran according to the volume-mass ratio of 1:10, the composite microbial inoculum is added according to 0.8% to 1.5% of the mass of the pile, and the preferred composite microbial inoculum is added according to 1.0% to 1.2% of the mass of the pile.|[0016] Further, mycorrhizal inoculant is added to the compost product which is putrescence, and then mixed with silicate mineral according to (0.5-1.2):100, preferably, and mixed with silicate mineral according to (0.8-1.0):100; the silicate mineral is crushed to a particle size of 200 μm-5mm, and preferably, the silicate mineral is crushed to a particle size of 600 μm-3mm.|[0017] Furthermore, the mycorrhizal inoculant and the compost product are evenly mixed according to the proportion of (2-5):100, and preferably, the mycorrhizal inoculant and the compost product are evenly mixed according to the proportion of (4-5):100; the preparation method of the mycorrhizal inoculant is that: the strain Glomus is prepared mosseae and Glomus The versiorm is propagated in a pot of clover in advance, and the mycorrhizal inoculant containing mycorrhizal fungi spores, extra-rhizosphere mycelium, infected root sections and rhizosphere soil is prepared.|[0018] Further, the silicate mineral is a combination of the calcium-based silicate tailings and any of feldspar, illite and wollastonite according to a mass ratio of 1:(2-5), and preferably, according to a mass ratio of 1:(4-5).|[0019] Furthermore, the compost product added with the mycorrhizal inoculant is mixed with silicate minerals and then is laid flat to a shallow plate reactor, and the layer thickness is 1.0cm to 3.0cm, and preferably, the layer thickness is 2.0 to 3.0cm.|[0020] Furthermore, urban sewage, non-point source wastewater or diluted organic wastewater are sprayed to the shallow flat reactor, and the humidity of the mixture layer is kept at 35% to 55%, and preferably, the humidity of the mixture layer is kept at 40% to 50%.|[0021] Further, the equipment used for the composting treatment is a drum-type device; the time for the composting treatment is 15 days; the invention utilizes the drum-type device to carry out the composting treatment according to the prior art.|[0022] Further, the volume fraction of CO2 in the CO2 containing mixed gas is 0.04% to 0.05%, and the invention is introduced with the mixed gas containing 0.04% to 0.05%CO2 to carry out carbon fixation reaction.|[0023] Compared with the prior art, the invention has the following technical effects:|[0024] (1) The invention utilizes the compost products with rich microbial population structure to accelerate the weathering of silicate minerals and improve the carbon fixing effect thereof, thereby realizing the multiple effect effects of organic waste fixation and resource utilization, ecological restoration in mining areas and CO2 fixation, and having good economic, environmental and social benefits.|[0025] (2) The invention adjusts the C/N ratio of the composting system by mixing sludge and cow dung, and adds bulking agent and tempering agent to carry out mixed composting; the obtained product contains dissolved organic substances such as protein, saccharide, hydrophilic organic acid and the like, and is beneficial to the growth, propagation and metabolism of silicate bacteria and fungi composite microorganisms, and accelerates the process of weathering and carbon fixation reaction of silicate minerals.|Specific Implementation Methods|[0026] The invention is further illustrated in the following specific embodiments, with detailed embodiments and operating procedures, but the scope of protection of the invention is not limited to the content.|[0027] Example 1|[0028] (1) The remaining sludge of the sewage plant and cow dung are mixed according to a ratio of 3:1, and granular corn stalks which are crushed to nearly 1cm are added according to a ratio of 6% of the mass of the obtained sludge-cow dung mixture; meanwhile, 75μm potash feldspar ore powder is added according to a ratio of 1.0% of the mass of the sludge-cow dung mixture; after fully mixed, dried composting products are added to adjust the initial water content of the composting mixture to 65%; and then a roller-type device is adopted to carry out composting treatment according to the prior art for 15d.|[0029] (2) The reactor is transferred to the cooling stage after the temperature rises to high temperature. When the temperature of the reactor is reduced to 36~40°C, a composite microbial inoculum with mass of 1.0% is added. The inoculum comprises Bacillus mucilaginosus and Aspergillus niger. The effective colony quantity ratio of the two inoculums is 1:6. After mixing, the inoculum is adsorbed evenly with bran according to the volume-mass ratio of 1:10. Then the inoculum is added into the reactor.|[0030] (3) After composting, the mycorrhizal inoculant was added into the composting product according to the mass ratio of 5:100. The preparation of mycorrhizal inoculant was as follows:The strain Glomus was selected as strain mosseae and Glomus The versiorm is cultivated in a clover pot, and the mycorrhizal inoculant containing mycorrhizal fungi spores, extra-root hypha, infected root sections and rhizosphere soil is prepared.|[0031] (4) The mixture of step (3) and the silicate mineral with a particle size of 600 μm are uniformly mixed according to a ratio of 1:100, and the silicate mineral consists of calcium-based silicate tailings and feldspar minerals according to a mass ratio of 1:2.|[0032] (5) The mixed materials obtained in step (4) are laid flat to a shallow flat reactor to form a material layer with a height of 2 cm. Urban sewage is periodically sprayed to maintain the moisture and humidity of the material layer at 40%, and CO2 volume fraction 0.05% mixed gas is introduced for carbon sequestration reaction.|[0033] The control group was set up, and the silicate minerals were directly laid out to the shallow flat reactor according to the step (4) to form a 2 cm height material layer. The municipal sewage was used to spray the water humidity of the material layer at 40% regularly, and the mixed gas of CO2 with the same concentration was introduced into the test group to carry out carbon fixation reaction. The concentration of CO2 in the gas phase at the upper part of the material layer was monitored in a sealed plate reactor. After 12h, the concentration of CO2 in the upper gas phase of the plate reactor decreased by 22.6% in the test group, while the decrease value of the control group was only 0.5%.|[0034] Example 2|[0035] (1) The remaining sludge of the sewage plant and the cow dung are mixed according to a ratio of 2:1, and rice straw with a length of about 1.5cm is added according to a ratio of 4% of the mass of the obtained sludge-cow dung mixture, and at the same time, calcium feldspar ore powder is added according to a ratio of 1.2% of the mass of the sludge-cow dung mixture, and composting treatment is carried out according to the prior art.|[0036] (2) When the reactor temperature is reduced to 38°C, a composite microbial inoculum of 1.3% mass of the reactor mixture is added, the effective colony quantity ratio of Bacillus mucilaginosus and Aspergillus niger is 1:8, and the mixed microbial inoculum is mixed with bran and absorbed evenly, and then added into the reactor.|[0037] (3) After composting, the mycorrhizal inoculant was added into the composting product according to the mass ratio of 2:100.|[0038] (4) The mixture of step (3) is uniformly mixed with silicate minerals with a particle size of 3mm according to a ratio of 1.2:100, and the silicate minerals consist of calcium-based silicate tailings and wollastonite minerals according to a mass ratio of 1:5.|[0039] (5) The mixed materials obtained in step (4) are laid flat to a shallow plate reactor to form a material layer with a height of 3 cm. The surface source sewage of greenhouse planting is periodically sprayed to keep the moisture and humidity of the material layer to be 55%, and the mixed gas with 0.04% of the volume fraction of CO2 is introduced to carry out the carbon fixation reaction.|[0040] A control group is arranged, and silicate minerals are directly laid on a shallow flat plate reactor according to step (4) to form a material layer with a height of 3cm; the surface source sewage of greenhouse planting is periodically sprayed to keep the water humidity of the material layer to be 55%; and the mixed gas with 0.04% of the volume fraction of CO2 is introduced to carry out the carbon fixation reaction. The remaining operations were the same as in Example 1. After 12h, the concentration of CO2 in the upper gas phase of the plate reactor decreased by 21.3% in the test group, but only 0.6% in the control group.|[0041] Example 3|[0042] (1) The remaining sludge of the sewage plant is mixed with the cow dung, mixed straws (wheat straws are mixed with corn straws in a ratio of 8% by weight of the obtained sludge-cow dung mixture) are added, feldspar ore powder (potassium feldspar ore powder is mixed with calcium feldspar ore powder in a ratio of 0.8% by weight of the sludge-cow dung mixture) is added, and compost treatment is carried out according to the prior art.|[0043] (2) When the reactor temperature is reduced to 38°C, a composite microbial inoculum of 0.8% mass of the reactor mixture is added, the effective colony quantity ratio of the bacillus mucilaginosus and the aspergillus niger is 1:6, and the mixed microbial inoculum is evenly mixed with bran for adsorption, and then added into the reactor.|[0044] (3) After composting, the mycorrhizal inoculant was added into the composting product according to the mass ratio of 4:100.|[0045] (4) The mixture of step (3) and the silicate mineral with the particle size of 1.5mm are uniformly mixed according to the proportion of 0.8:100, and the silicate mineral consists of the calcium-based silicate tailings and illite ore powder according to the proportion of 1:4 by mass.|[0046] (5) The mixed materials obtained in step (4) are laid flat to a shallow plate reactor to form a material layer with a height of 1.5cm. The waste water from citric acid production is diluted to a chemical oxygen demand of 400mg/L and then periodically sprayed to keep the moisture and humidity of the material layer at 35%, and the mixed gas with 0.04% of the volume fraction of CO2 is introduced to carry out carbon fixation reaction.|[0047] A control group was set up, and silicate minerals were directly laid out to a shallow plate reactor according to step (4) to form a material layer with a height of 1.5cm. The wastewater from citric acid production was diluted to a chemical oxygen demand of 400mg/L and then sprayed regularly to keep the moisture of the material layer at 35%, and the mixed gas with 0.04% CO2 volume fraction was introduced to conduct carbon fixation reaction. The remaining operations were the same as in Example 1. After 12h, the concentration of CO2 in the upper gas phase of the plate reactor decreased by 26.2% in the test group, but only 0.3% in the control group.|[0048] In spite of that exhaustive description of the present invention, the above embodiment are only some but not all embodiments of the present invention, and other embodiments may be obtain without being creative according to the present embodiment, which are all within the scope of the present invention. Family Number|(105090822)|105090822|Abstract|(CN116161660 A)|The invention discloses a technical method for improving silicate mineral carbon sequestration potential by sludge - cow dung mixed composting , which comprises the following steps : mixing residual sludge of a sewage plant with cow dung , adding a swelling agent and a conditioning agent for composting treatment , and adding a bacillus mucilaginosus and aspergillus niger compound microbial agent when the temperature of a pile body is reduced from a high - temperature stage to a medium - temperature state ; the method comprises the following steps : adding a mycorrhiza inoculant into a decomposed compost product , mixing with silicate minerals according to a mass ratio of ( 0.5-1.2 ) : 100, spreading the mixture in a shallow plate reactor , spraying municipal sewage , non - point source wastewater or diluted organic wastewater to keep the moisture humidity of a mixture layer at 35-55%, and introducing CO2 - containing mixed gas to carry out a carbon sequestration reaction . The compost product which is rich in organic matter and beneficial to growth and reproduction of compound microorganisms is prepared , weathering of silicate minerals is accelerated , the carbon sequestration effect of the silicate minerals is improved , and the multiple effects of organic matter waste recycling , mining area ecological restoration and CO2 immobilization are achieved . |(WO2024169718 A1)|Disclosed in the present invention is a technique for improving the carbon sequestration potential of silicate minerals by means of sludge-cow dung mixed composting. The technique comprises: mixing residual sludge of a sewage plant with cow dung, adding a bulking agent and a conditioning agent for a composting treatment, adding a composite microbial agent of Bacillus mucilaginosus and Aspergillus niger when the temperature of the compost is reduced to a medium-temperature state from a high-temperature stage, adding a mycorrhizal inoculant to the decomposed compost product, then mixing same with silicate minerals in a mass ratio of (0.5-1.2):100, paving the resulting mixture into a shallow plate reactor, spraying with urban sewage, non-point source wastewater or diluted organic wastewater to keep the moisture of the mixed material layer at 35-55%, and introducing mixed gas containing CO2 for a carbon sequestration reaction. In the present invention, the compost product that is rich in organic matter and good for growth and reproduction of composite microorganisms is prepared, and the weathering of silicate minerals is accelerated and the carbon sequestration effect of the silicate minerals is improved, thus achieving multiple action effects of organic matter waste recycling, mining area ecological restoration and CO2 sequestration.|CPC codes|(CN116161660 A)|C01B - 032/55 |(WO2024169718 A1)|C01B-032/55|IPC codes|(CN116161660 A)|C01B - 032/55 |(WO2024169718 A1)|C01B-032/55|Title|(CN116161660 A)|Technical method for improving silicate mineral carbon sequestration potential through sludge - cow dung mixed compost |(WO2024169718 A1)|Technique for improving carbon sequestration potential of silicate minerals by means of sludge-cow dung mixed composting| Materials, metallurgy C01B-032/55|Y02W-030/40 C01B-032/55|Y02W-030/40 C01B-032/55 C01B-032/55 WO2024169718|CN118901538|CN117716968B WO2024169718 105090822 WHO=Examiner SELF=Y CAT=P CAT=X|CN118901538 112129557 WHO=Examiner SELF=N CAT=A|CN117716968B 108922854 WHO=Examiner SELF=N CN115591395|CN102775201|CN116161660|CN115504811|CN115591395|CN115245073|CN114669585|CN115010550|US20220259041|US20210285017|CN107226730|US20160023959|WO201197183|CN101407437|WO2007111479|JP2007112669 CN115591395 103441127 WHO=Examiner SELF=N CAT=Y|CN102775201 7988639 WHO=Examiner SELF=N CAT=Y|CN116161660 105090822 WHO=Examiner SELF=Y CAT=P CAT=X|CN115504811 103126524 WHO=Examiner SELF=N CAT=A|CN115591395 103441127 WHO=Examiner SELF=N CAT=A|CN115245073 102320301 WHO=Examiner SELF=N CAT=A|CN114669585 100668033 WHO=Examiner SELF=N CAT=A|CN115010550 101667900 WHO=Examiner SELF=N CAT=A|US20220259041 92125648 WHO=Examiner SELF=N CAT=A|US20210285017 79372628 WHO=Examiner SELF=N CAT=A|CN107226730 77399566 WHO=Examiner SELF=N CAT=A|US20160023959 72083599 WHO=Examiner SELF=N CAT=A|WO201197183 44624013 WHO=Examiner SELF=N CAT=A|CN101407437 6743402 WHO=Examiner SELF=N CAT=A|WO2007111479 34185180 WHO=Examiner SELF=N CAT=A|JP2007112669 32567711 WHO=Examiner SELF=N CAT=A 张继舟: &quot;污泥源蚓粪及其生物炭对Cd2+/Pb2+的吸附行为研究&quot;, 中国博士学位论文全文数据库, 1 December 2020 (2020-12-01) (Cat. A)|宁平: &quot;冶金化工废气高值资源化利用关键技术及应用&quot;, 中国环保产业, 26 February 2022 (2022-02-26) (Cat. A)|周文静;潘辰;连宾;: &quot;环境污染加剧石质文物风化:机理、过程及防护措施&quot;, 地球与环境, no. 04, 15 August 2013 (2013-08-15) (Cat. A) CN116161660; CN114669585; CN115010550; CN115591395; CN115245073; JP2007112669; US20210285017; WO2007111479|CN101407437; WO201197183; CN102775201; US20160023959; CN107226730; US20220259041; CN115504811; CN115591395 |(CN116161660)|Search Report references [Examiner]|-TERVAHAUTA, T: "Black water sludge reuse in agriculture: Are heavy metals a problem?", JOURNAL OF HAZAROUS MATERIALS, 15 June 2014 (2014-06-15)| PENDING (WO2024/169718)|PENDING|(CN116161660)|LAPSED ALIVE (WO2024/169718)|ALIVE|(CN116161660)|DEAD (WO2024/169718)|LEGAL DETAILS FOR WO2024/169718|Actual or expected expiration date=2026-08-16|Legal state=ALIVE|Status=PENDING|Event publication date=2024-02-05|Event code=WO/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=WO WOCN2024/075922|Application date=2024-02-05|Standardized application number=2024WO-CN75922|Event publication date=2024-08-22|Event code=WO/A1|Event group=Examination events|Published application with search report|Publication country=WO|Publication number=WO2024/169718|Publication stage code=A1|Publication date=2024-08-22|Standardized publication number=WO2024169718|MEMBER STATE LEGAL DETAILS FOR DE|Actual or expected expiration date=2025-09-17|Legal state=DEAD|Status=LAPSED|Corresponding cc:|Designated or member state=DE|Event publication date=2025-09-17|Event code=WO/NENP|Event group=Event indicating Not In Force|Non-entry into the national phase|Corresponding cc:|Designated or member state=DE|MEMBER STATE LEGAL DETAILS FOR EP|Actual or expected expiration date=2026-02-11|Legal state=DEAD|Status=LAPSED|Corresponding cc:|Designated or member state=EP Corresponding appl: EP24756092|Event publication date=2024-10-02|Event code=WO/121|Event group=Designated states|EP: The EPO has been informed by wipo that ep was designated in this application|Corresponding cc:|Designated or member state=EP|Event publication date=2026-02-11|Event code=WO/122|Event indicator=Neg|Event group=Event indicating Not In Force|EP: PCT app. not ent. europ. phase|EP: PCT anmeldung nicht in europaeische phase eingetreten|Corresponding cc:|Designated or member state=EP|(CN116161660)|LEGAL DETAILS FOR CN116161660|Actual or expected expiration date=2025-03-18|Legal state=DEAD|Status=LAPSED|Event publication date=2023-02-16|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202310125395|Application date=2023-02-16|Standardized application number=2023CN-0125395|Event publication date=2023-05-26|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN116161660|Publication stage code=A|Publication date=2023-05-26|Standardized publication number=CN116161660|Event publication date=2023-05-26|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-06-13|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-03-18|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication (WO2024/169718)|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW|(WO2024/169718)|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ|(WO2024/169718)|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR|(WO2024/169718)|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML|(WO2024/169718)|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (WO2024/169718)|WO https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCDq9NuAxM7mYt0P/F2Pwh1EkaV0SMUACwOCCKReMmHu7M9Ry4MrhQjLALkMBz8hwaI=&n=1 http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2024169718&redirectedID=true https://permalink.orbit.com/RenderStaticFirstPage?XPN=LaL9ujorV6yRa%252FCxTvISU7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (WO2024/169718)|CN|(CN116161660)|CN (WO2024/169718)|NAME=KUNMING UNIVERSITY OF SCIENCE AND TECHNOLOGY Kunming University Of Science And Technology, Chenggong District Kunming, Yunnan 650500 , COUNTRY=CN|(CN116161660)|NAME=KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (WO2024/169718)|CN| (WO2024/169718)|NAME=BEIJING GAOWO LAW FIRM Room 602, 6 Floor, No.11 Caihefang Road Haidian District, Beijing 100080 , POSTCODE=100080 , COUNTRY=CN|(CN116161660)|NAME=ZHANG YU;Kunming Tongju Patent Agency Co., Ltd. , REG=53214 (WO2024/169718)|CN; CN; CN; CN; CN; CN; CN| (WO2024/169718)|NAME=LIU, Shugen Kunming University Of Science And Technology, Chenggong District Kunming, Yunnan 650500, POSTCODE=650500, COUNTRY=CN |NAME=WANG, Qionghui Kunming University Of Science And Technology, Chenggong District Kunming, Yunnan 650500, POSTCODE=650500, COUNTRY=CN |NAME=TIAN, Senlin Kunming University Of Science And Technology, Chenggong District Kunming, Yunnan 650500, POSTCODE=650500, COUNTRY=CN |NAME=SUN, Yi Kunming University Of Science And Technology, Chenggong District Kunming, Yunnan 650500, POSTCODE=650500, COUNTRY=CN |NAME=PENG, Yuxin Kunming University Of Science And Technology, Chenggong District Kunming, Yunnan 650500, POSTCODE=650500, COUNTRY=CN |NAME=NING, Ping Kunming University Of Science And Technology, Chenggong District Kunming, Yunnan 650500, POSTCODE=650500, COUNTRY=CN |NAME=LI, Yingjie Kunming University Of Science And Technology, Chenggong District Kunming, Yunnan 650500, POSTCODE=650500, COUNTRY=CN|(CN116161660)|NAME=LIU SHUGEN|NAME=WANG QIONGHUI|NAME=TIAN SENLIN|NAME=SUN YI|NAME=PENG YUXIN|NAME=NING PING|NAME=LI YINGJIE 12 2 Titre: (WO2024/169718)|Technique for improving carbon sequestration potential of silicate minerals by means of sludge-cow dung mixed composting Résumé: (WO2024/169718)|Disclosed in the present invention is a technique for improving the carbon sequestration potential of silicate minerals by means of sludge-cow dung mixed composting. The technique comprises: mixing residual sludge of a sewage plant with cow dung, adding a bulking agent and a conditioning agent for a composting treatment, adding a composite microbial agent of Bacillus mucilaginosus and Aspergillus niger when the temperature of the compost is reduced to a medium-temperature state from a high-temperature stage, adding a mycorrhizal inoculant to the decomposed compost product, then mixing same with silicate minerals in a mass ratio of (0.5-1.2):100, paving the resulting mixture into a shallow plate reactor, spraying with urban sewage, non-point source wastewater or diluted organic wastewater to keep the moisture of the mixed material layer at 35-55%, and introducing mixed gas containing CO2 for a carbon sequestration reaction. In the present invention, the compost product that is rich in organic matter and good for growth and reproduction of composite microorganisms is prepared, and the weathering of silicate minerals is accelerated and the carbon sequestration effect of the silicate minerals is improved, thus achieving multiple action effects of organic matter waste recycling, mining area ecological restoration and CO2 sequestration. 6 Abstract gpt-4o-mini yes The article describes a technique that explicitly aims to improve carbon sequestration through the weathering of silicate minerals, involving microbial agents and the introduction of CO2, which aligns with the topic of enhanced weathering.
14 CN201811456532 CN201811456532 CN109368643 83478532 CN109368643 A 2019-02-22 [CN109368643] 2018-11-30 2018-11-30 2019-02-22 (CN109368643)|2024-05-17 (CN109368643)|Carbon sequestration method by means of AOD slag (CN109368643)|The invention relates to a carbon sequestration method by means of AOD steel slag. The method comprises the following steps that 1, the AOD steel slag is subjected to crushing treatment, and then screening, drying and cooling treatment is conducted; 2, the treated steel slag is placed in a reaction kettle, and deionized water is added, wherein a ratio of the deionized water to the steel slag is (6to 8) L/Kg; 3, CO2 is introduced into the reaction kettle, after CO2 partial pressure is 7-9 bar, a valve is closed, and temperature is elevated to 120-140 DEG C to start reaction; 4, after the reaction is completed, gas in the kettle is released, after the kettle is cooled to a room temperature, slurry subjected to the reaction is poured out, and filtered, and filter residues are placed in a drying box for drying. The carbon dioxide absorptivity of the AOD steel slag subjected to carbon sequestration is 12.62-15.73%, discharge of carbon dioxide is greatly reduced, and meanwhile, the waste AOD steel slag is subjected to secondary utilization, so that resource recycling is fully achieved. NORTH CHINA UNIVERSITY OF SCIENCE & TECHNOLOGY (CN109368643)|NORTH CHINA UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) LI JUNGUO|CENG YANAN|WANG YAJUN (CN109368643)|LI JUNGUO|CENG YANAN|WANG YAJUN (CN109368643)|XU DONGFENG;XIAMEN YUANCHUANG INTELLECTUAL PROPERTY FIRM (GENERAL PARTNERSHIP)|Reg. Nb: 35101 (CN109368643)|Influence of partial pressure of carbon dioxide on AOD slag carbon sequestration: research shows that when the partial pressure of carbon dioxide is less than 7bar, the carbon fixing capacity of the AOD slag is increased along with the increase of the partial pressure of the carbon dioxide, and basically tends to be in a stable state after the partial pressure of the carbon dioxide exceeds 7bar, but the AOD slag starts to show a reduced state after the partial pressure of the carbon dioxide exceeds 10bar, because the carbonation process of the steel slag conforms to an unreacted shrinkage core model, the generated calcium carbonate can cover the surface of slag particles, the porosity of the slag particles is reduced, the process is further accelerated by higher pressure, and the dense carbonate and SiO are rapidly generated on the surface of the particles2Protective layer of CO2Is difficult to access the inside of the particle, therebyThe reaction is reduced.| (CN109368643)|1. A method for carbon fixation by using AOD steel slag is characterized by comprising the following steps: the method comprises the following steps:1) carrying out crushing treatment on the AOD steel slag, and then carrying out screening, drying and cooling treatment;2) putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is (8-10) L/Kg;3) introducing CO into the reaction kettle2To be treated with CO2Closing the valve when the partial pressure is 7-9bar, and heating to 140-160 ℃ to start reaction;4) and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a drying oven.| (CN109368643)|Based on the background, the invention provides a method for carbon fixation by using AOD steel slag, which aims to reduce airMiddle CO2The steel slag waste is recycled while being discharged.|The application relates to a method for fixing carbon by using AOD steel slagThe method comprises the following steps: 1. carrying out crushing treatment on the AOD steel slag, and then carrying out screening, drying and cooling treatment; 2. putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is (6-8) L/Kg; 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 7-9bar, and heating to 120-140 ℃ to start reaction; 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a drying oven.|The invention relates to a method for fixing carbon by steel slag, in particular to a method for fixing carbon by AOD slag.| (CN109368643)|STEEL SLAG(100,22)|AOD SLAG(100,11)|AOD STEEL SLAG(100,9)|CARBON FIXATION(100,7)|STEEL SLAGTHE(68,1)|REACTION KETTLE2TO(60,7)|SLURRY REACTION(60,7)|DRYING OVEN(56,9)|TREATED STEEL SLAG(54,7)|REACTION KETTLE(52,7)|METHANEDIONE EMISSION(49,2)|COOLING TREATMENT(46,3)|TERNARY ALKALINITY(44,2)|FIXING CARBON(44,1)|FILTER RESIDUE(43,7)|RESOURCE RECYCLING(42,2)|CRUSHED STEEL SLAG(40,2)|KETTLE(38,7)|WASTE AOD(38,2)|DEIONIZED WATER(25,15)|CRUSHED AOD STEEL SLAG(24,4)|MGO(16,8)|AOD SLAG CARBON SEQUESTRATION(15,2)|DRIED AOD(13,4)|AL2O(12,6)|PARTIAL PRESSURE(11,7)|FEO(11,6)|CARRYING OUT CRUSHING TREATMENT(11,3)|CARRYING OUT SCREENING(11,3)|200 MESH SCREEN(11,2)|CARBONATION ACCELERATION(11,1)|ROOM TEMPERATURE(10,11)|STAINLESS STEEL SLAG(9,4)|CONSTANT TEMPERATURE(9,2)|METHANEDIONE CONTENT(9,2)|CHIMNEY MYRIAD(9,1)|METHANEDIONE ABSORPTION(9,1)|SOUTH POLE MELT(9,1)|GLOBAL CLIMATE ANOMALY(8,1)|LAND DROUGHT(8,1)|ROUGH ESTIMATE(8,1)|FINAL METHANEDIONE UPTAKE RATE(7,2)|DRYING TIME(6,2)|AOD SLAG RATIO(6,1)|CARBONATION REACTION(6,1)|CO2THE DISCHARGE REDUCTION(6,1)|FORMED3THE CONTENT(6,1)|INSOLUBLE CARBONATE(6,1)|LIQUID FILM2THE(6,1)|RESOURCE WASTE(6,1)|SLAG PARTICLE(6,1)|200 MESH SIEVE(5,4)|INORGANIC PHASE(5,2)|ATMOSPHERIC POLLUTION INFLUENCE(5,1)|CALCIUM HYDRATION REACTION(5,1)|CO2THE REACTION(5,1)|SYSTEM2CO3DECOMPOSITION(5,1)|ANIMAL HUSBANDRY(4,1)|DISSOLUTION(4,1)|ELUTION(4,1)|EXPERT(4,1)|FISHERY(4,1)|FIXED METHANEDIONE(4,1)| (CN109368643)|1. A method for carbon fixation by using AOD steel slag is characterized by comprising the following steps: the method comprises the following steps:|1) carrying out crushing treatment on the AOD steel slag, and then carrying out screening, drying and cooling treatment;|2) putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is (8-10) L/Kg;|3) introducing CO into the reaction kettle2To be treated with CO2Closing the valve when the partial pressure is 7-9bar, and heating to 140-160 ℃ to start reaction;|4) and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a drying oven.|2. The method of claim 1, wherein: the reaction time in the step 3) is controlled to be more than 1 h.|3. The method of any of claims 1-2, wherein: the ternary alkalinity ((CaO + MgO)/SiO) of the AOD slag2) Is 2.2-2.8.|4. The method of any one of claims 1-3, wherein: the AOD slag comprises the following components: CaO 51-55%, SiO222-25%、MgO 4-8%、Al2O31-3%、FeO 1-2%、TiO20.6-0.8%、MnO 0.1-0.3%、Cr 0.5-0.8%、V 0.008-0.009%。|5. The method of claim 4, wherein: the drying in the step 4) is constant temperature drying in a drying oven with the temperature of 100-120 ℃, and the preferred drying time is 6-8 hours.|6. The method of claim 4, wherein: the screening is to screen the crushed steel slag through a 200-mesh screen. (CN109368643)|TECHNICAL FIELD|[0002] The invention relates to a method for fixing carbon by steel slag, in particular to a method for fixing carbon by AOD slag.|BACKGROUND ART|[0004] In recent years, people gradually pay attention to the influence of atmospheric pollution on global climate change. Through research, it is considered that carbon dioxide plays a significant role in various air pollutants that may cause climate change. The large amount of carbon dioxide emitted into the atmosphere from the myriad of chimneys and other waste gas pipelines on earth, about 50% remains in the atmosphere. Carbon dioxide absorbs long wave radiation from the ground, raising the temperature of the air near the ground floor, which is called the "greenhouse effect". According to rough estimation, if the content of carbon dioxide in the atmosphere is increased by 25%, the temperature of the near-ground air can be increased by 0.5-2 ℃. If the temperature is increased by 100 percent, the temperature near the ground can be increased by 1.5 to 6 ℃. Some experts believe that the carbon dioxide content in the atmosphere increases at the present rate, and several years later, ice in the north and south poles melts, resulting in global climate anomalies. Studies have shown that the global average air temperature will rise by 1.4 to 5.8 degrees celsius from 1900 to 2100 years. The fact that global warming has the greatest harm to agricultural production is the fact that the global warming is not in conflict, the food crisis is caused by drought of land and reduced yield of crops, but unexpectedly, nine major industries such as fishery, forestry, mining, animal husbandry, energy industry and the like are greatly influenced, so that the reduction of CO2The discharge of (2) is already urgent for the current environmental protection.|[0005] According to statistics, the yield of stainless steel crude steel in China in this year is about 2500 ten thousand tons, and 850 ten thousand tons of stainless steel slag can be generated according to 1 ton of steel slag generated by every 3 tons of steel, so that the utilization degree of the stainless steel slag in China is extremely low, most of the stainless steel slag is naturally stacked, a large amount of space is occupied, and resource waste is caused. However, AOD slag as stainless steel slag contains alkali metal ions capable of reacting with CO2The reaction takes place to form insoluble carbonate, and CO is finally removed2And (4) fixing.|DISCLOSURE|[0006] Disclosure of Invention|[0007] Based on the background, the invention provides a method for carbon fixation by using AOD steel slag, which aims to reduce airMiddle CO2The steel slag waste is recycled while being discharged.|[0008] In order to achieve the purpose, the technical scheme adopted by the invention is as follows:|[0009] a method for carbon fixation by using AOD steel slag comprises the following steps:|[0010] 1. carrying out crushing treatment on the AOD steel slag, and then carrying out screening, drying and cooling treatment;|[0011] 2. putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is (8-10) L/Kg;|[0012] 3. introducing CO into the reaction kettle2To be treated with CO2Closing the valve when the partial pressure is 7-9bar, and heating to 140-160 ℃ to start reaction;|[0013] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a drying oven.|[0014] Further, the screening is to screen the crushed steel slag through a 200-mesh screen.|[0015] Further, the drying in the step 4 is constant temperature drying in a drying oven at 120 ℃ and 100 ℃, and the drying time is preferably 6-8 hours.|[0016] Furthermore, the reaction time in step 3 is controlled to be more than 1 h.|[0017] Further, the ternary alkalinity ((CaO + MgO)/SiO) of the AOD slag2) Is 2.2-2.8.|[0018] Further, the AOD slag comprises the following components: CaO 51-55%, SiO222-25%、MgO 4-8%、Al2O31-3%、FeO 1-2%、TiO20.6-0.8%、MnO 0.1-0.3%、Cr 0.5-0.8%、V 0.008-0.009%。|[0019] Influence of reaction temperature on AOD slag carbon sequestration: the study showed that at temperatures below 140 ℃ the dissolution of the Ca-containing mineral phase increasedCO decomposition2The amount of the AOD slag dissolved in the aqueous solution increases with the increase in temperature, and reaches a saturation level at 140 ℃ while the temperature exceeds 160 ℃ due to H in the system2CO3Decomposition of (2) with reduction of CO32+And further the carbon fixing ability of the AOD slag is reduced. Therefore, in order to ensure the optimal carbon fixing capacity, the reaction temperature is optimally controlled at 140 ℃ to 160 ℃.|[0020] Influence of deionized water to AOD slag ratio (liquid-solid ratio) on AOD slag carbon sequestration: the key to the carbonation is CO2Ca dissolved in water and coming out of solid phase2+Binding to form calcium carbonate. On the one hand, the water can promote the hydration reaction of the calcium-containing mineral phase in the steel slag, so that more Ca is generated2+Dissolution and further acceleration of carbonation. But CO is hindered when the moisture is excessive2Reach the surface of slag particles to react with CO2Decomposition of and Ca2+The elution is carried out on a liquid film on the surface of the solid matter, and when the liquid-solid ratio is high, CO is inhibited2So that the CO reaches the liquid film2The concentration is reduced, thereby resulting in CaCO being formed3The content of (a) is reduced, and finally the fixed carbon dioxide amount of the AOD slag is not too much. Meanwhile, the existence of excessive water can reduce the mass transmission process of the whole reaction, so that the concentration of ions participating in the reaction is reduced, and the proceeding of the carbonation reaction is further influenced. Based on the content of Ca in the AOD slag, the liquid-solid ratio is controlled to be (8-10) L/Kg.|[0021] Influence of partial pressure of carbon dioxide on AOD slag carbon sequestration: research shows that when the partial pressure of carbon dioxide is less than 7bar, the carbon fixing capacity of the AOD slag is increased along with the increase of the partial pressure of the carbon dioxide, and basically tends to be in a stable state after the partial pressure of the carbon dioxide exceeds 7bar, but the AOD slag starts to show a reduced state after the partial pressure of the carbon dioxide exceeds 10bar, because the carbonation process of the steel slag conforms to an unreacted shrinkage core model, the generated calcium carbonate can cover the surface of slag particles, the porosity of the slag particles is reduced, the process is further accelerated by higher pressure, and the dense carbonate and SiO are rapidly generated on the surface of the particles2Protective layer of CO2Is difficult to access the inside of the particle, therebyThe reaction is reduced.|[0022] The invention has the beneficial effects that: the absorption rate of carbon dioxide after the AOD steel slag is solidified is 16.88-19.52%, the emission of carbon dioxide is greatly reduced, and meanwhile, the waste AOD steel slag is recycled, so that the resource recycling is fully realized.|INVENTION MODE|[0023] Detailed Description|[0024] The technical effect of the present invention and the absorption rate of carbon dioxide referred to in the following examples are calculated as follows:wherein, the delta m is the difference between the quality of the steel slag after the step 4 and the quality of the steel slag after the step 1; and m is the mass of the steel slag after the step 1 is finished.|INVENTION MODE|[0025] Example 1|[0026] A method for carbon fixation by using AOD steel slag comprises the following steps:|[0027] 1. crushing AOD steel slag, sieving the crushed AOD steel slag by a 200-mesh sieve, drying the crushed AOD steel slag at 80 ℃, and cooling the dried AOD steel slag to room temperature, wherein the AOD steel slag comprises the following components: CaO 51%, SiO222%、MgO 4%、Al2O31%、FeO 1%、TiO20.6%、MnO 0.1%、Cr 0.5%、V 0.008%;|[0028] 2. Putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is 8L/Kg;|[0029] 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 7bar, heating to 140 ℃ and starting to react for 1 h;|[0030] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a drying oven at 100 ℃ for 6 hours.|[0031] The final carbon dioxide uptake rate, measured by the above method, was 16.84%.|INVENTION MODE|[0032] Example 2|[0033] A method for carbon fixation by using AOD steel slag comprises the following steps:|[0034] 1. crushing AOD steel slag, sieving the crushed AOD steel slag by a 200-mesh sieve, drying the crushed AOD steel slag at 90 ℃ and cooling the dried AOD steel slag to room temperature, wherein the AOD steel slag comprises the following components: CaO 53%, SiO223%、MgO 5%、Al2O32%、FeO1.4%、TiO20.8%、MnO 0.3%、Cr 0.6%、V 0.008%;|[0035] 2. Putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is 9L/Kg;|[0036] 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 7bar, heating to 155 ℃, and starting to react for 1 h;|[0037] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a 120 ℃ drying oven for 8 hours.|[0038] The final carbon dioxide uptake rate, measured by the above method, was 18.02%.|INVENTION MODE|[0039] Example 3|[0040] A method for carbon fixation by using AOD steel slag comprises the following steps:|[0041] 1. crushing AOD steel slag, sieving the crushed AOD steel slag by a 200-mesh sieve, drying the crushed AOD steel slag at 90 ℃ and cooling the dried AOD steel slag to room temperature, wherein the AOD steel slag comprises the following components: CaO 55%, SiO224%、MgO 8%、Al2O33%、FeO 2%、TiO20.8%、MnO 0.3%、Cr 0.8%、V 0.009%CaO 40%;|[0042] 2. Putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is 10L/Kg;|[0043] 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 8bar, heating to 160 ℃, and starting to react for 1.5 h;|[0044] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a 120 ℃ drying oven for 8 hours.|[0045] The absorption of carbon dioxide was finally metered in by the above-described method to be 19.41%.|INVENTION MODE|[0046] Example 4|[0047] A method for carbon fixation by using AOD steel slag comprises the following steps:|[0048] 1. crushing AOD steel slag, sieving the crushed AOD steel slag by a 200-mesh sieve, drying the crushed AOD steel slag at 100 ℃, and cooling the dried AOD steel slag to room temperature, wherein the AOD steel slag comprises the following components: 54% of CaO and SiO225%、MgO 4%、Al2O33%、FeO 2%、TiO20.77%、MnO 0.26%、Cr 0.72%、V 0.009%;|[0049] 2. Putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is 9L/Kg;|[0050] 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 7.2bar, heating to 145 ℃ and starting to react for 2.5 h;|[0051] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a 120 ℃ drying oven for 6 hours.|[0052] The final metering by the above method gave an absorption of 16.89% of carbon dioxide.|[0053] The foregoing is merely exemplary and illustrative of the present invention and various modifications, additions and substitutions may be made by those skilled in the art to the specific embodiments described without departing from the scope of the invention as defined in the following claims. (CN109368643)|TECHNICAL FIELD|[0002] The invention relates to a method for fixing carbon by steel slag, in particular to a method for fixing carbon by AOD slag.|BACKGROUND ART|[0004] In recent years, people gradually pay attention to the influence of atmospheric pollution on global climate change. Through research, it is considered that carbon dioxide plays a significant role in various air pollutants that may cause climate change. The large amount of carbon dioxide emitted into the atmosphere from the myriad of chimneys and other waste gas pipelines on earth, about 50% remains in the atmosphere. Carbon dioxide absorbs long wave radiation from the ground, raising the temperature of the air near the ground floor, which is called the "greenhouse effect". According to rough estimation, if the content of carbon dioxide in the atmosphere is increased by 25%, the temperature of the near-ground air can be increased by 0.5-2 ℃. If the temperature is increased by 100 percent, the temperature near the ground can be increased by 1.5 to 6 ℃. Some experts believe that the carbon dioxide content in the atmosphere increases at the present rate, and several years later, ice in the north and south poles melts, resulting in global climate anomalies. Studies have shown that the global average air temperature will rise by 1.4 to 5.8 degrees celsius from 1900 to 2100 years. The fact that global warming has the greatest harm to agricultural production is the fact that the global warming is not in conflict, the food crisis is caused by drought of land and reduced yield of crops, but unexpectedly, nine major industries such as fishery, forestry, mining, animal husbandry, energy industry and the like are greatly influenced, so that the reduction of CO2The discharge of (2) is already urgent for the current environmental protection.|[0005] According to statistics, the yield of stainless steel crude steel in China in this year is about 2500 ten thousand tons, and 850 ten thousand tons of stainless steel slag can be generated according to 1 ton of steel slag generated by every 3 tons of steel, so that the utilization degree of the stainless steel slag in China is extremely low, most of the stainless steel slag is naturally stacked, a large amount of space is occupied, and resource waste is caused. However, AOD slag as stainless steel slag contains alkali metal ions capable of reacting with CO2The reaction takes place to form insoluble carbonate, and CO is finally removed2And (4) fixing.|DISCLOSURE|[0006] Disclosure of Invention|[0007] Based on the background, the invention provides a method for carbon fixation by using AOD steel slag, which aims to reduce airMiddle CO2The steel slag waste is recycled while being discharged.|[0008] In order to achieve the purpose, the technical scheme adopted by the invention is as follows:|[0009] a method for carbon fixation by using AOD steel slag comprises the following steps:|[0010] 1. carrying out crushing treatment on the AOD steel slag, and then carrying out screening, drying and cooling treatment;|[0011] 2. putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is (8-10) L/Kg;|[0012] 3. introducing CO into the reaction kettle2To be treated with CO2Closing the valve when the partial pressure is 7-9bar, and heating to 140-160 ℃ to start reaction;|[0013] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a drying oven.|[0014] Further, the screening is to screen the crushed steel slag through a 200-mesh screen.|[0015] Further, the drying in the step 4 is constant temperature drying in a drying oven at 120 ℃ and 100 ℃, and the drying time is preferably 6-8 hours.|[0016] Furthermore, the reaction time in step 3 is controlled to be more than 1 h.|[0017] Further, the ternary alkalinity ((CaO + MgO)/SiO) of the AOD slag2) Is 2.2-2.8.|[0018] Further, the AOD slag comprises the following components: CaO 51-55%, SiO222-25%、MgO 4-8%、Al2O31-3%、FeO 1-2%、TiO20.6-0.8%、MnO 0.1-0.3%、Cr 0.5-0.8%、V 0.008-0.009%。|[0019] Influence of reaction temperature on AOD slag carbon sequestration: the study showed that at temperatures below 140 ℃ the dissolution of the Ca-containing mineral phase increasedCO decomposition2The amount of the AOD slag dissolved in the aqueous solution increases with the increase in temperature, and reaches a saturation level at 140 ℃ while the temperature exceeds 160 ℃ due to H in the system2CO3Decomposition of (2) with reduction of CO32+And further the carbon fixing ability of the AOD slag is reduced. Therefore, in order to ensure the optimal carbon fixing capacity, the reaction temperature is optimally controlled at 140 ℃ to 160 ℃.|[0020] Influence of deionized water to AOD slag ratio (liquid-solid ratio) on AOD slag carbon sequestration: the key to the carbonation is CO2Ca dissolved in water and coming out of solid phase2+Binding to form calcium carbonate. On the one hand, the water can promote the hydration reaction of the calcium-containing mineral phase in the steel slag, so that more Ca is generated2+Dissolution and further acceleration of carbonation. But CO is hindered when the moisture is excessive2Reach the surface of slag particles to react with CO2Decomposition of and Ca2+The elution is carried out on a liquid film on the surface of the solid matter, and when the liquid-solid ratio is high, CO is inhibited2So that the CO reaches the liquid film2The concentration is reduced, thereby resulting in CaCO being formed3The content of (a) is reduced, and finally the fixed carbon dioxide amount of the AOD slag is not too much. Meanwhile, the existence of excessive water can reduce the mass transmission process of the whole reaction, so that the concentration of ions participating in the reaction is reduced, and the proceeding of the carbonation reaction is further influenced. Based on the content of Ca in the AOD slag, the liquid-solid ratio is controlled to be (8-10) L/Kg.|[0021] Influence of partial pressure of carbon dioxide on AOD slag carbon sequestration: research shows that when the partial pressure of carbon dioxide is less than 7bar, the carbon fixing capacity of the AOD slag is increased along with the increase of the partial pressure of the carbon dioxide, and basically tends to be in a stable state after the partial pressure of the carbon dioxide exceeds 7bar, but the AOD slag starts to show a reduced state after the partial pressure of the carbon dioxide exceeds 10bar, because the carbonation process of the steel slag conforms to an unreacted shrinkage core model, the generated calcium carbonate can cover the surface of slag particles, the porosity of the slag particles is reduced, the process is further accelerated by higher pressure, and the dense carbonate and SiO are rapidly generated on the surface of the particles2Protective layer of CO2Is difficult to access the inside of the particle, therebyThe reaction is reduced.|[0022] The invention has the beneficial effects that: the absorption rate of carbon dioxide after the AOD steel slag is solidified is 16.88-19.52%, the emission of carbon dioxide is greatly reduced, and meanwhile, the waste AOD steel slag is recycled, so that the resource recycling is fully realized.|INVENTION MODE|[0023] Detailed Description|[0024] The technical effect of the present invention and the absorption rate of carbon dioxide referred to in the following examples are calculated as follows:wherein, the delta m is the difference between the quality of the steel slag after the step 4 and the quality of the steel slag after the step 1; and m is the mass of the steel slag after the step 1 is finished.|INVENTION MODE|[0025] Example 1|[0026] A method for carbon fixation by using AOD steel slag comprises the following steps:|[0027] 1. crushing AOD steel slag, sieving the crushed AOD steel slag by a 200-mesh sieve, drying the crushed AOD steel slag at 80 ℃, and cooling the dried AOD steel slag to room temperature, wherein the AOD steel slag comprises the following components: CaO 51%, SiO222%、MgO 4%、Al2O31%、FeO 1%、TiO20.6%、MnO 0.1%、Cr 0.5%、V 0.008%;|[0028] 2. Putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is 8L/Kg;|[0029] 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 7bar, heating to 140 ℃ and starting to react for 1 h;|[0030] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a drying oven at 100 ℃ for 6 hours.|[0031] The final carbon dioxide uptake rate, measured by the above method, was 16.84%.|INVENTION MODE|[0032] Example 2|[0033] A method for carbon fixation by using AOD steel slag comprises the following steps:|[0034] 1. crushing AOD steel slag, sieving the crushed AOD steel slag by a 200-mesh sieve, drying the crushed AOD steel slag at 90 ℃ and cooling the dried AOD steel slag to room temperature, wherein the AOD steel slag comprises the following components: CaO 53%, SiO223%、MgO 5%、Al2O32%、FeO1.4%、TiO20.8%、MnO 0.3%、Cr 0.6%、V 0.008%;|[0035] 2. Putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is 9L/Kg;|[0036] 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 7bar, heating to 155 ℃, and starting to react for 1 h;|[0037] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a 120 ℃ drying oven for 8 hours.|[0038] The final carbon dioxide uptake rate, measured by the above method, was 18.02%.|INVENTION MODE|[0039] Example 3|[0040] A method for carbon fixation by using AOD steel slag comprises the following steps:|[0041] 1. crushing AOD steel slag, sieving the crushed AOD steel slag by a 200-mesh sieve, drying the crushed AOD steel slag at 90 ℃ and cooling the dried AOD steel slag to room temperature, wherein the AOD steel slag comprises the following components: CaO 55%, SiO224%、MgO 8%、Al2O33%、FeO 2%、TiO20.8%、MnO 0.3%、Cr 0.8%、V 0.009%CaO 40%;|[0042] 2. Putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is 10L/Kg;|[0043] 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 8bar, heating to 160 ℃, and starting to react for 1.5 h;|[0044] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a 120 ℃ drying oven for 8 hours.|[0045] The absorption of carbon dioxide was finally metered in by the above-described method to be 19.41%.|INVENTION MODE|[0046] Example 4|[0047] A method for carbon fixation by using AOD steel slag comprises the following steps:|[0048] 1. crushing AOD steel slag, sieving the crushed AOD steel slag by a 200-mesh sieve, drying the crushed AOD steel slag at 100 ℃, and cooling the dried AOD steel slag to room temperature, wherein the AOD steel slag comprises the following components: 54% of CaO and SiO225%、MgO 4%、Al2O33%、FeO 2%、TiO20.77%、MnO 0.26%、Cr 0.72%、V 0.009%;|[0049] 2. Putting the treated steel slag into a reaction kettle, and adding deionized water, wherein the ratio of the deionized water to the steel slag is 9L/Kg;|[0050] 3. introducing CO into the reaction kettle2To be treated with CO2Closing a valve when the partial pressure is 7.2bar, heating to 145 ℃ and starting to react for 2.5 h;|[0051] 4. and after the reaction is finished, discharging the gas in the kettle, cooling to room temperature, pouring out the reacted slurry, filtering, and drying the filter residue in a 120 ℃ drying oven for 6 hours.|[0052] The final metering by the above method gave an absorption of 16.89% of carbon dioxide.|[0053] The foregoing is merely exemplary and illustrative of the present invention and various modifications, additions and substitutions may be made by those skilled in the art to the specific embodiments described without departing from the scope of the invention as defined in the following claims. Family Number|(83478532)|83478532|Abstract|(CN109368643 A)|The invention relates to a carbon sequestration method by means of AOD steel slag . The method comprises the following steps that 1, the AOD steel slag is subjected to crushing treatment , and then screening , drying and cooling treatment is conducted ; 2, the treated steel slag is placed in a reaction kettle , and deionized water is added , wherein a ratio of the deionized water to the steel slag is ( 6 to 8 ) L / Kg ; 3, CO2 is introduced into the reaction kettle , after CO2 partial pressure is 7-9 bar , a valve is closed , and temperature is elevated to 120-140 DEG C to start reaction ; 4, after the reaction is completed , gas in the kettle is released , after the kettle is cooled to a room temperature , slurry subjected to the reaction is poured out , and filtered , and filter residues are placed in a drying box for drying . The carbon dioxide absorptivity of the AOD steel slag subjected to carbon sequestration is 12.62-15.73%, discharge of carbon dioxide is greatly reduced , and meanwhile , the waste AOD steel slag is subjected to secondary utilization , so that resource recycling is fully achieved . |CPC codes|(CN109368643 A)|C01B - 032/55 |IPC codes|(CN109368643 A)|C01B - 032/55 |Title|(CN109368643 A)|Carbon sequestration method by means of AOD slag | Materials, metallurgy C01B-032/55 C01B-032/55 C01B-032/55 C01B-032/55 CN119040529B CN119040529B 112403288 WHO=Examiner SELF=N CN101851071|CN103111186|CN102671519|CN101219330|CN101269920|US20120134902|JP2005097072|JP2003134958 CN101851071 7094502 WHO=Examiner SELF=N CAT=Y CAT=X|CN103111186 73658034 WHO=Examiner SELF=N CAT=X|CN102671519 7857479 WHO=Examiner SELF=N CAT=X|CN101219330 6570309 WHO=Examiner SELF=N CAT=X|CN101269920 62147640 WHO=Examiner SELF=N CAT=X|US20120134902 7717288 WHO=Examiner SELF=N CAT=A|JP2005097072 22202253 WHO=Examiner SELF=N CAT=A|JP2003134958 31813637 WHO=Examiner SELF=N CAT=A 涂茂霞等: &quot;水淬钢渣碳酸化固定CO2&quot;, 《环境工程学报》 (Cat. X)|WOUTER J.J. 等: &quot;Mineral CO2 sequestration by steel slag carbonation&quot;, 《ENVIRON.SCI.TECHNOL.》 (Cat. Y,X) JP2003134958; JP2005097072; CN101219330; CN101269920; US20120134902; CN102671519; CN103111186; CN101851071 REVOKED (CN109368643)|REVOKED DEAD (CN109368643)|DEAD (CN109368643)|LEGAL DETAILS FOR CN109368643|Actual or expected expiration date=2024-05-17|Legal state=DEAD|Status=REVOKED|Event publication date=2018-11-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201811456532|Application date=2018-11-30|Standardized application number=2018CN-1456532|Event publication date=2019-02-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN109368643|Publication stage code=A|Publication date=2019-02-22|Standardized publication number=CN109368643|Event publication date=2019-02-22|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2019-03-19|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-05-17|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjkRm7G7Abl74Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000022572208&ekey=2218&xpn=CN109368643&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=m6KxXZ1V3Ak2l2OVb%252B3JU5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN109368643)|CN (CN109368643)|NAME=NORTH CHINA UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN109368643)|NAME=XU DONGFENG;XIAMEN YUANCHUANG INTELLECTUAL PROPERTY FIRM (GENERAL PARTNERSHIP) , REG=35101 (CN109368643)|NAME=LI JUNGUO|NAME=CENG YANAN|NAME=WANG YAJUN 0 1 Titre: (CN109368643)|Carbon sequestration method by means of AOD slag Résumé: (CN109368643)|The invention relates to a carbon sequestration method by means of AOD steel slag. The method comprises the following steps that 1, the AOD steel slag is subjected to crushing treatment, and then screening, drying and cooling treatment is conducted; 2, the treated steel slag is placed in a reaction kettle, and deionized water is added, wherein a ratio of the deionized water to the steel slag is (6to 8) L/Kg; 3, CO2 is introduced into the reaction kettle, after CO2 partial pressure is 7-9 bar, a valve is closed, and temperature is elevated to 120-140 DEG C to start reaction; 4, after the reaction is completed, gas in the kettle is released, after the kettle is cooled to a room temperature, slurry subjected to the reaction is poured out, and filtered, and filter residues are placed in a drying box for drying. The carbon dioxide absorptivity of the AOD steel slag subjected to carbon sequestration is 12.62-15.73%, discharge of carbon dioxide is greatly reduced, and meanwhile, the waste AOD steel slag is subjected to secondary utilization, so that resource recycling is fully achieved. 14 Abstract gpt-4o-mini no The method focuses on carbon sequestration using AOD steel slag but does not involve the accelerated weathering of silicate or alkaline minerals for CO₂ capture.
15 CN202410538454 CN202410538454 CN118267851 110443660 CN118267851 A 2024-07-02 [CN118267851] 2024-04-30 2024-04-30 2024-07-02 (CN118267851)|2044-04-30 (CN118267851)|Method for carbon sequestration by using sintering machine head ash modified steel slag (CN118267851)|The invention discloses a method for carbon sequestration by using sintering machine head ash modified steel slag, and belongs to the technical field of industrial solid waste treatment and environmental protection. According to the carbon sequestration method, steel slag is crushed and screened to obtain steel slag powder, then the steel slag powder and sintering machine head ash are ground according to a certain proportion to obtain modified steel slag powder, and finally the modified steel slag powder is used for direct carbon sequestration. By adopting the technical scheme provided by the invention, the carbon sequestration capability of the steel slag can be obviously improved, the purpose of capturing CO2 by using the steel slag is effectively realized, and meanwhile, a good way is provided for utilizing the steel slag and the sintering machine head ash. ANHUI UNIVERSITY OF TECHNOLOGY (CN118267851)|ANHUI UNIVERSITY OF TECHNOLOGY ([CN]) LONG HONGMING|FAN CHUNLONG|WEI RUFEI|SUN RONG|DING RAN|ZHANG HAO|DI ZHANXIA (CN118267851)|LONG HONGMING|FAN CHUNLONG|WEI RUFEI|SUN RONG|DING RAN|ZHANG HAO|DI ZHANXIA (CN118267851)|SHANG XIANFANG;WEN PARTNERS P.C.|Reg. Nb: 34134 (CN118267851)|As another example, the application of chinese patent application number 202210599827.3 discloses a method for carbon sequestration and emission reduction of steel slag in a steel plant, and the application is that the steel slag is crushed into powder, then is prepared into steel slag slurry, and finally the steel slag slurry, stabilizer and flue gas are introduced into a ball mill together for wet milling, thereby fixing CO 2, but the method is complex in process and low in carbon sequestration capability. Meanwhile, 2 CaO.SiO 2 and CaO.SiO 2 in the steel slag are not easy to generate carbonation reaction in the prior art, main active components of the steel slag and CO 2 in carbonation reaction are CaO and Ca (OH) 2, and the contents of the two components in the steel slag are greatly lower than the content of silicate, so that the carbon fixation amount of the steel slag is limited, and the large-scale application of the steel slag for carbon fixation is limited.|The addition amount of the sintering machine head ash is too low, so that the structural stability of C 2 S in the steel slag is difficult to be reduced due to too little K +; too high an amount of the sintering head ash causes excessive K + to block the diffusion of Ca 2+, thereby inhibiting the gas-solid reaction from proceeding, and conversely causing the reduction of the carbon-fixing capacity of the steel slag.| (CN118267851)|1. A method for carbon fixation by utilizing sintering machine head ash modified steel slag is characterized in that: crushing and screening the steel slag, grinding the obtained steel slag powder and sintering machine head ash to obtain modified steel slag powder, roasting the modified steel slag powder, and introducing CO 2 for carbon fixation while roasting.| (CN118267851)|In a further preferred aspect of the present invention, in the second step, the added mass of the sintering head ash is 1% of the mass of the steel slag powder.|The invention discloses a method for carbon fixation by utilizing sintering machine head ash modified steel slag, and belongs to the technical fields of industrial solid waste treatment and environmental protection.|The invention provides a method for carbon fixation by utilizing sintering machine head ash modified steel slag, which comprises the steps of crushing and screening the steel slag to obtain steel slag powder, grinding the steel slag powder and the sintering machine head ash according to a certain proportion to obtain modified steel slag powder, roasting the modified steel slag powder, and introducing CO 2 to carry out carbon fixation while roasting.| (CN118267851)|STEEL SLAG(100,107)|CARBON FIXATION(100,62)|SINTERING MACHINE HEAD ASH(100,60)|STEEL SLAG POWDER(77,36)|SINTERING HEAD ASH(56,2)|STEEL SLAG SLURRY(53,2)|SLAG POWDER(42,37)|CARBONATION REACTION(38,3)|CARBON SEQUESTRATION(35,10)|MODIFIED STEEL SLAG POWDER(34,36)|SLAG POWDER CRUSHING(34,1)|CORUNDUM CRUCIBLE(31,20)|REMAINDER UNAVOIDABLE IMPURITY(31,2)|CRUSHING(29,4)|STEEL SLAG UTILIZATION(27,2)|CARBON SEQUESTRATION CAPABILITY(24,1)|STEEL SLAG EMISSION REDUCTION(23,1)|MACHINE HEAD ASH(22,14)|ROASTING(20,27)|PROCEEDING(18,1)|STABILIZER(18,1)|CAO SIO(16,1)|ADDED MASS(15,2)|ENVIRONMENTAL PROTECTION(14,2)|STEEL SLAG ACTIVE COMPONENT(14,1)|BALL MILL(13,1)|WET MILLING(13,1)|CARBON FIXING CAPABILITY(12,2)|SOLID WASTE TREATMENT(12,2)|MUFFLE FURNACE(11,20)|AL2O(11,11)|EMISSION REDUCTION(11,1)|MGO(10,11)|CRUCIBLE MASS(10,6)|CARBON FIXING CAPACITY(10,5)|FLUE GAS(10,1)|PLANETARY BALL MILL(8,12)|FE2O(8,9)|K2O(8,2)|NESTED SUBRANGE(8,2)|STRUCTURAL STABILITY(8,2)|CARBON FIXATION CAPACITY(7,8)|ROTATING SPEED(7,7)|SELF BURNING LOSS(7,5)|STEEL PLANT(6,8)|EXPERIMENT(6,6)|SOLID WASTE(6,4)|GAS SOLID REACTION(6,2)|ACTIVE COMPONENT(6,1)|HETEROATOM INVASION(6,1)|STEEL SLAG ADOPTION(6,1)|STEEL SLAG CARBONATION(6,1)|STEEL SLAG MODIFIER(6,1)|STEEL SLAG RECYCLING UTILIZATION(6,1)|CARBON FIXING TEMPERATURE(5,5)|JAW CRUSHER(5,5)|HUMAN INDUSTRIALIZATION(5,1)|RECYCLING RESOURCE(5,1)|STEEL SLAG MODIFICATION(5,1)|LARGE PARTICLE IMPURITY(4,7)|P2O(4,6)|STEEL SLAG CARBON FIXATION(4,2)|CYCLICAL UTILIZATION(4,1)|DOPING DEFECT(4,1)|LATTICE CHEMICAL DEFECT(4,1)|LATTICE STABILITY(4,1)|OXYGEN VACANCY DEFECT(4,1)|UNREACTED CALCIUM(4,1)|GRAIN SIZE(3,7)|GRINDING TIME(3,7)|PARTICLE SIZE(3,7)|RAW MATERIAL(3,7)|LARGE SCALE CHANGE(3,5)|SIO2(3,5)|R MIN(3,2)|CAO REACTION(3,1)|ELECTRONIC CONDUCTIVITY(3,1)|ELECTRONIC MOBILITY(3,1)|GROUND STEEL SLAG(3,1)|LEGAL EQUIVALENT(3,1)|RECYCLING TREATMENT(3,1)| (CN118267851)|1. A method for carbon fixation by utilizing sintering machine head ash modified steel slag is characterized in that: crushing and screening the steel slag, grinding the obtained steel slag powder and sintering machine head ash to obtain modified steel slag powder, roasting the modified steel slag powder, and introducing CO 2 for carbon fixation while roasting.|2. The method for carbon sequestration using the sintering machine head ash modified steel slag according to claim 1, characterized in that: the method comprises the following steps:| Step one, raw material preparation |(1) Preparation of slag powder|Crushing, grinding and screening the steel slag to obtain steel slag powder with the grain size of 100-200 meshes;| (2) Sintering machine head ash screening |Screening the sintering machine head ash to remove large-particle impurities to obtain sintering machine head ash with the particle size less than or equal to 100 meshes;| step two, preparing modified steel slag powder |Grinding the steel slag powder treated in the first step with sintering machine head ash to obtain modified steel slag powder;| step three, carbon fixation is carried out by using modified steel slag powder |Introducing CO 2 at a certain temperature to directly fix carbon in the modified steel slag powder.|3. The method for carbon sequestration using the sintering machine head ash modified steel slag according to claim 2, characterized in that: in the second step, the added mass of the sintering machine head ash is 1-10% of the mass of the steel slag powder.|4. The method for carbon sequestration using the sintering machine head ash modified steel slag according to claim 2, characterized in that: in the second step, a planetary ball mill is adopted for grinding, the rotating speed is controlled to be 500-800 r/min, and the grinding time is 0.5-1.5 h.|5. The method for carbon sequestration using the sintering machine head ash modified steel slag according to claim 2, characterized in that: in the third step, the flow rate of the introduced CO 2 is 500-1000 mL/min.|6. The method for carbon sequestration using the sintering machine head ash modified steel slag according to claim 2, characterized in that: in the third step, the carbon fixing temperature is 650-750 ℃ and the carbon fixing time is 1-2 h.|7. The method for carbon sequestration using the ash modified steel slag from sintering machine head according to any one of claims 1 to 5, characterized in that: the components of the steel slag comprise :CaO36.60～65.85%、SiO22.17～24.94%、Al2O32.91～28.85%、MgO2.99～7.61%、Fe2O31.74～28.22%、P2O50.05～2.50%, and the balance of unavoidable impurities.|8. The method for carbon sequestration using the ash modified steel slag from sintering machine head according to any one of claims 1 to5, characterized in that: the constituents of the sinter head ash include :Fe 10～40%、K2O5～30%、Na2O0.6～5%、MgO 0.5～3%、SiO20.3～5%、CaO1～12%、Al2O31～4%、Cl 5～25%, the remainder unavoidable impurities. (CN118267851)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of industrial solid waste treatment and environmental protection, and particularly relates to a method for carbon fixation by utilizing sintering machine head ash modified steel slag.|BACKGROUND ART|[0002] With the development and progress of human industrialization, the emission amount of CO 2 is continuously increased, and thus the global warming problem is increasingly serious, and how to reduce carbon emission and suppress global warming is a hot spot of human interest.|[0003] The carbonation of the steel slag not only can utilize the solid waste steel slag of a steel plant to fix waste gas CO 2 nearby, but also can obviously reduce free oxides in the steel slag, promote the utilization of the steel slag as building materials and realize the treatment of waste by waste and cyclic utilization. However, the active ingredient in the steel slag, which can perform carbonation reaction with CO 2, is metal oxide such as f-CaO, and the total content of the active ingredient is low, so that a large amount of effective trapping of CO 2 cannot be realized.|[0004] Through searching, related patents related to the adoption of steel slag for carbon fixation are disclosed, for example, an application with the Chinese patent application number of 202211142705.8 discloses a steel slag carbon fixation device and a use method thereof, and the application simply increases the contact time of steel slag powder and CO 2 through the carbon fixation device to realize the carbon fixation of the steel slag, so that the carbon fixation capacity is lower.|[0005] As another example, the application of chinese patent application number 202210599827.3 discloses a method for carbon sequestration and emission reduction of steel slag in a steel plant, and the application is that the steel slag is crushed into powder, then is prepared into steel slag slurry, and finally the steel slag slurry, stabilizer and flue gas are introduced into a ball mill together for wet milling, thereby fixing CO 2, but the method is complex in process and low in carbon sequestration capability.|[0006] Meanwhile, 2 CaO.SiO 2 and CaO.SiO 2 in the steel slag are not easy to generate carbonation reaction in the prior art, main active components of the steel slag and CO 2 in carbonation reaction are CaO and Ca (OH) 2, and the contents of the two components in the steel slag are greatly lower than the content of silicate, so that the carbon fixation amount of the steel slag is limited, and the large-scale application of the steel slag for carbon fixation is limited. Therefore, the improvement of the carbon fixing capacity of the steel slag has important significance for capturing CO 2 and realizing the recycling utilization of the steel slag.|DISCLOSURE|Disclosure of Invention|[0007] 1. Problems to be solved|[0008] Aiming at the defects of lower carbon fixing capacity and lower carbon fixing amount when steel slag is adopted for carbon fixing in the prior art, the invention provides a method for carbon fixing by utilizing sintering machine head ash to modify steel slag, and the sintering machine head ash is used for modifying the steel slag, so that the problems are effectively solved.|[0009] 2. Technical proposal|[0010] In order to solve the problems, the technical scheme adopted by the invention is as follows:|[0011] The invention provides a method for carbon fixation by utilizing sintering machine head ash modified steel slag, which comprises the steps of crushing and screening the steel slag to obtain steel slag powder, grinding the steel slag powder and the sintering machine head ash according to a certain proportion to obtain modified steel slag powder, roasting the modified steel slag powder, and introducing CO 2 to carry out carbon fixation while roasting. |[0012] Specifically, the carbon fixing method of the invention comprises the following steps:|[0013] Step one, raw material preparation |[0014] (1) Preparation of slag powder|[0015] Crushing, grinding and screening the steel slag to obtain steel slag powder with the grain size of 100-200 meshes;|[0016] (2) Sintering machine head ash screening |[0017] Screening the sintering machine head ash to remove large-particle impurities to obtain sintering machine head ash with the particle size less than or equal to 100 meshes;|[0018] step two, preparing modified steel slag powder |[0019] Grinding the steel slag powder treated in the first step with sintering machine head ash to obtain modified steel slag powder;|[0020] Step three, roasting the modified steel slag powder and fixing carbon |[0021] And roasting the modified steel slag powder under the condition of introducing CO 2.|[0022] The steel slag used in the invention comprises :CaO36.60～65.85%、SiO22.17～24.94%、Al2O32.91～28.85%、MgO 2.99～7.61%、Fe2O31.74～28.22%、P2O50.05～2.50%, the rest of unavoidable impurities. When the steel slag is directly used for carbon fixation, the carbon fixation capacity is poor due to the poor activity of the steel slag, so that a large amount of CO 2 can not be captured by the steel slag. The constituents of the sinter head ash used include :Fe 10～40%、K2O5～30%、Na2O0.6～5%、MgO0.5～3%、SiO20.3～5%、CaO1～12%、Al2O31～4%、Cl 5～25%, the remainder unavoidable impurities.|[0023] The applicant finds that, through a great deal of research, the sintering machine head ash is doped into steel slag and is subjected to grinding treatment, so that the steel slag can be modified to improve the carbon fixing capability of the steel slag, and the main characteristics are that:|[0024] (1) The sintering machine head ash contains a large amount of metal K, the change of the atomic size of K doping modification positions can cause the contraction or expansion of crystal lattices, the length of a calcium-oxygen bond is changed, the band gap of an energy band is further influenced, and the electronic conductivity and the electronic mobility are changed; |[0025] (2) Invasion of the hetero atom decreases the lattice stability of C 2 S; |[0026] (3) Lattice chemical defects such as doping defects and oxygen vacancy defects are formed, so that ion mobility is improved, the diffusion rate of unreacted Ca 2+ through a CaCO 3 product layer on the surface is accelerated, and gas-solid reaction is promoted. |[0027] Therefore, after the sintering machine head ash is added into the steel slag, the structural stability of C 2 S in the steel slag can be effectively reduced through K modification, the reaction of C 2 S and CO 2 is promoted, and the carbon fixing capacity of the steel slag is improved, so that the purpose of treating waste by waste and recycling resources is realized.|[0028] In a further preferred aspect of the present invention, in the second step, the added mass of the sintering head ash is 1% of the mass of the steel slag powder. The addition amount of the sintering machine head ash is too low, so that the structural stability of C 2 S in the steel slag is difficult to be reduced due to too little K +; too high an amount of the sintering head ash causes excessive K + to block the diffusion of Ca 2+, thereby inhibiting the gas-solid reaction from proceeding, and conversely causing the reduction of the carbon-fixing capacity of the steel slag.|[0029] In the second step, a planetary ball mill is adopted for grinding, the rotating speed is controlled to be 500-800 r/min, and the grinding time is 0.5-1.5 h.|[0030] As a further preferred aspect of the present invention, in the third step, the flow rate of CO 2 to 1000mL/min is introduced.|[0031] As a further preferable mode of the invention, in the third step, the carbon fixing temperature is 650-750 ℃ and the carbon fixing time is 1-2 h. The carbon fixing temperature has an influence on the carbon fixing capacity of the steel slag, and CaCO 3 is generated by utilizing the reaction of CaO and CO 2 in the modified steel slag when the carbon is fixed in the modified steel slag. When the carbon fixing temperature is lower than the requirement of the invention, the carbon fixing reaction may not be carried out or the reaction is incomplete, so that the carbon fixing effect is affected, and when the carbon fixing temperature is higher than the requirement of the invention, caCO 3 is decomposed and CO 2 is generated.|[0032] 3. Advantageous effects|[0033] Compared with the prior art, the invention has the beneficial effects that:|[0034] According to the method for carbon fixation by utilizing the sintering machine head ash to modify the steel slag, the sintering machine head ash is utilized to modify the steel slag, so that the carbon fixation capacity of the steel slag is remarkably improved, the treatment cost is low, and the method is suitable for industrial large-scale application. |[0035] Meanwhile, the sintering machine head ash is used as a steel slag modifier, so that a new thought suitable for recycling treatment is found for the solid waste sintering machine head ash of the steel plant, and the treatment of waste by waste is realized.|INVENTION MODE|Detailed Description|[0036] The invention is further described below in connection with specific embodiments.|[0037] Example 1|[0038] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0039] Step one, raw material preparation |[0040] (1) Preparation of slag powder|[0041] Crushing the steel slag by adopting a jaw crusher, and grinding and screening to obtain steel slag powder with the grain size of 200 meshes.|[0042] (2) Sintering machine head ash screening|[0043] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0044] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities.|[0045] Step two, preparing modified steel slag powder|[0046] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 3% of that of the steel slag powder, the rotating speed of the planetary ball mill is 650r/min, and the grinding time is 1h. And grinding to obtain modified steel slag powder.|[0047] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0048] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0049] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, so that the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass of the crucible is weighed and recorded as m 4, the mass difference before and after the carbon fixation is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1. |[0050] Example 2|[0051] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0052] Step one, raw material preparation |[0053] (1) Preparation of slag powder|[0054] Crushing the steel slag by adopting a jaw crusher, and grinding and sieving to obtain steel slag powder with the grain size of 100-200 meshes.|[0055] (2) Sintering machine head ash screening|[0056] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0057] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities. However, the present embodiment is described by taking the above specific raw material composition as an example, but the specific composition of each raw material is not limited to the present embodiment.|[0058] Step two, preparing modified steel slag powder|[0059] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 1% of that of the steel slag powder, the rotating speed of the planetary ball mill is 500r/min, and the grinding time is 1.5h. And grinding to obtain modified steel slag powder.|[0060] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0061] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0062] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, so that the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass is weighed and recorded as m 4, the mass difference before and after roasting is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1. |[0063] Example 3|[0064] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0065] Step one, raw material preparation |[0066] (1) Preparation of slag powder|[0067] Crushing the steel slag by adopting a jaw crusher, and grinding and sieving to obtain steel slag powder with the grain size of 100-200 meshes.|[0068] (2) Sintering machine head ash screening|[0069] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0070] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities. However, the present embodiment is described by taking the above specific raw material composition as an example, but the specific composition of each raw material is not limited to the present embodiment.|[0071] Step two, preparing modified steel slag powder|[0072] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 10% of that of the steel slag powder, the rotating speed of the planetary ball mill is 800r/min, and the grinding time is 0.5h. And grinding to obtain modified steel slag powder.|[0073] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0074] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0075] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, so that the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass is weighed and recorded as m 4, the mass difference before and after roasting is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1. |[0076] Example 4|[0077] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0078] Step one, raw material preparation |[0079] (1) Preparation of slag powder|[0080] Crushing the steel slag by adopting a jaw crusher, and grinding and sieving to obtain steel slag powder with the grain size of 100-200 meshes.|[0081] (2) Sintering machine head ash screening|[0082] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0083] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities. However, the present embodiment is described by taking the above specific raw material composition as an example, but the specific composition of each raw material is not limited to the present embodiment.|[0084] Step two, preparing modified steel slag powder|[0085] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 1% of that of the steel slag powder, the rotating speed of the planetary ball mill is 650r/min, and the grinding time is 1h. And grinding to obtain modified steel slag powder.|[0086] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0087] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 650 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0088] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 650 ℃ for roasting, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass is weighed and recorded as m 4, the mass difference before and after roasting is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1.|[0089] Example 5|[0090] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0091] Step one, raw material preparation |[0092] (1) Preparation of slag powder|[0093] Crushing the steel slag by adopting a jaw crusher, and grinding and sieving to obtain steel slag powder with the grain size of 100-200 meshes.|[0094] (2) Sintering machine head ash screening|[0095] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0096] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities. However, the present embodiment is described by taking the above specific raw material composition as an example, but the specific composition of each raw material is not limited to the present embodiment.|[0097] Step two, preparing modified steel slag powder|[0098] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 1% of that of the steel slag powder, the rotating speed of the planetary ball mill is 650r/min, and the grinding time is 1h. And grinding to obtain modified steel slag powder.|[0099] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0100] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 750 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0101] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 750 ℃ for roasting, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, so that the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass is weighed and recorded as m 4, the mass difference before and after roasting is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1. |[0102] Example 6|[0103] The procedure of this example 1 is basically the same as that of example 1, and the difference between this example 1 is that: the components of the steel slag and the sintering machine head ash adopted are different, and specifically, the steel slag used in the embodiment comprises the following components:|[0104] CaO36.60%、SiO23.14%、Al2O3228.85%、MgO 7.61%、Fe2O32.6%、P2O52.50%, The balance being unavoidable impurities. |[0105] The sinter head ash composition is as follows:|[0106] Fe 40%、K2O30%、Na2O4%、MgO 0.5%、SiO20.3%、CaO12%、Al2O34%、Cl 15%.|[0107] Example 8 |[0108] The procedure of this example 1 is basically the same as that of example 1, and the difference between this example 1 is that: the components of the steel slag and the sintering machine head ash adopted are different, and specifically, the steel slag used in the embodiment comprises the following components:|[0109] CaO36.8%、SiO224.94%、Al2O33.12%、MgO 2.99%、Fe2O328.22%、P2O50.15%, The balance being unavoidable impurities. |[0110] The sinter head ash composition is as follows:|[0111] Fe 20%、K2O28%、Na2O5%、MgO3%、SiO23%、CaO8%、Al2O32%、Cl 5%。|[0112] Comparative example 1 |[0113] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the sintering machine head ash is not added, the crushed and sieved steel slag is directly adopted, the roasting and carbon fixation are carried out under the condition of introducing CO 2, and after the experiment is finished, the experiment result record is shown in table 1.|[0114] Comparative example 2|[0115] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the sintering machine head ash is not added, but the steel slag powder is independently ground, and finally CO 2 is introduced into the ground steel slag for roasting and carbon fixation, and after the experiment is finished, experimental results are recorded as shown in table 1.|[0116] Comparative example 3|[0117] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the sintering machine head ash was added, but the steel slag and the sintering machine head ash were not ground, but were directly mixed, and after the experiment was completed, the experimental results were recorded as shown in table 1.|[0118] Comparative example 4|[0119] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the amounts of the added head ash were varied, specifically, the mass of the added head ash was 0.5% of the mass of the steel slag in this comparative example, and after the experiment was completed, the experimental results were recorded as shown in table 1.|[0120] Comparative example 5|[0121] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the amounts of the added head ash were different, specifically, the mass of the added head ash of the sintering machine in this comparative example was 11% of the mass of the steel slag, and after the experiment was completed, the experimental results were recorded as shown in table 1.|[0122] Table 1 carbon sequestration data for each example of the invention and each comparative example|[0123] Numbering devicem1/gm2/gma/gm3/gm4/gmb/gmf/gCarbon fixation ability/g/kgExample 115.22115.2180.00315.22115.2460.0250.02828Example 215.22115.2190.00215.22115.2440.0230.02525Example 315.22115.2160.00515.22115.2430.0220.02727Example 415.22115.2190.00215.22115.2440.0230.02525Example 515.22115.2190.00215.22115.2430.0220.02424Example 615.22115.2170.00415.22115.2430.0220.02626Example 715.22115.2180.00315.22115.2420.0210.02424Example 815.22115.2190.00215.22115.2460.0250.02727Comparative example 115.22115.2180.00315.22115.2290.0080.01111Comparative example 215.22115.2170.00415.22115.2300.0090.01313Comparative example 315.22115.2180.00315.22115.2350.0140.01717Comparative example 415.22115.2190.00215.22115.2310.0100.01212Comparative example 515.22115.2160.00515.22115.2250.0040.0099|[0124] More specifically, although exemplary embodiments of the present invention have been described herein, the present invention is not limited to these embodiments, but includes any and all embodiments that have been modified, omitted, e.g., combined, adapted, and/or substituted between the various embodiments, as would be recognized by those skilled in the art in light of the foregoing detailed description. The limitations in the claims are to be interpreted broadly based on the language employed in the claims and not limited to examples described in the foregoing detailed description or during the prosecution of the application, which examples are to be construed as non-exclusive. Any steps recited in any method or process claims may be executed in any order and are not limited to the order presented in the claims. The scope of the invention should, therefore, be determined only by the appended claims and their legal equivalents, rather than by the descriptions and examples given above.|[0125] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. In case of conflict, the present specification, definitions, will control. Where a rate, pressure, temperature, time, or other value or parameter is expressed as a range, preferred range, or as a range bounded by a list of upper and lower preferred values, this is to be understood as specifically disclosing all ranges formed from any pair of any upper range limit or preferred value and any lower range limit or preferred value, regardless of whether ranges are separately disclosed. For example, a range of 1-50 should be understood to include any number, combination of numbers, or subranges selected from 1、2、3、4、5、6、7、8、9、10、11、12、13、14、15、16、17、18、19、20、21、22、23、24、25、26、27、28、29、30、31、32、33、34、35、36、37、38、39、40、41、42、43、44、45、46、47、48、49 or 50, and all fractional values between the integers described above, e.g., 1.1, 1.2, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8, and 1.9. Regarding sub-ranges, specifically considered are "nested sub-ranges" that extend from any end point within the range. For example, the nested subranges of exemplary ranges 1-50 can include 1-10, 1-20, 1-30, and 1-40 in one direction, or 50-40, 50-30, 50-20, and 50-10 in another direction. (CN118267851)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of industrial solid waste treatment and environmental protection, and particularly relates to a method for carbon fixation by utilizing sintering machine head ash modified steel slag.|BACKGROUND ART|[0002] With the development and progress of human industrialization, the emission amount of CO 2 is continuously increased, and thus the global warming problem is increasingly serious, and how to reduce carbon emission and suppress global warming is a hot spot of human interest.|[0003] The carbonation of the steel slag not only can utilize the solid waste steel slag of a steel plant to fix waste gas CO 2 nearby, but also can obviously reduce free oxides in the steel slag, promote the utilization of the steel slag as building materials and realize the treatment of waste by waste and cyclic utilization. However, the active ingredient in the steel slag, which can perform carbonation reaction with CO 2, is metal oxide such as f-CaO, and the total content of the active ingredient is low, so that a large amount of effective trapping of CO 2 cannot be realized.|[0004] Through searching, related patents related to the adoption of steel slag for carbon fixation are disclosed, for example, an application with the Chinese patent application number of 202211142705.8 discloses a steel slag carbon fixation device and a use method thereof, and the application simply increases the contact time of steel slag powder and CO 2 through the carbon fixation device to realize the carbon fixation of the steel slag, so that the carbon fixation capacity is lower.|[0005] As another example, the application of chinese patent application number 202210599827.3 discloses a method for carbon sequestration and emission reduction of steel slag in a steel plant, and the application is that the steel slag is crushed into powder, then is prepared into steel slag slurry, and finally the steel slag slurry, stabilizer and flue gas are introduced into a ball mill together for wet milling, thereby fixing CO 2, but the method is complex in process and low in carbon sequestration capability.|[0006] Meanwhile, 2 CaO.SiO 2 and CaO.SiO 2 in the steel slag are not easy to generate carbonation reaction in the prior art, main active components of the steel slag and CO 2 in carbonation reaction are CaO and Ca (OH) 2, and the contents of the two components in the steel slag are greatly lower than the content of silicate, so that the carbon fixation amount of the steel slag is limited, and the large-scale application of the steel slag for carbon fixation is limited. Therefore, the improvement of the carbon fixing capacity of the steel slag has important significance for capturing CO 2 and realizing the recycling utilization of the steel slag.|DISCLOSURE|Disclosure of Invention|[0007] 1. Problems to be solved|[0008] Aiming at the defects of lower carbon fixing capacity and lower carbon fixing amount when steel slag is adopted for carbon fixing in the prior art, the invention provides a method for carbon fixing by utilizing sintering machine head ash to modify steel slag, and the sintering machine head ash is used for modifying the steel slag, so that the problems are effectively solved.|[0009] 2. Technical proposal|[0010] In order to solve the problems, the technical scheme adopted by the invention is as follows:|[0011] The invention provides a method for carbon fixation by utilizing sintering machine head ash modified steel slag, which comprises the steps of crushing and screening the steel slag to obtain steel slag powder, grinding the steel slag powder and the sintering machine head ash according to a certain proportion to obtain modified steel slag powder, roasting the modified steel slag powder, and introducing CO 2 to carry out carbon fixation while roasting. |[0012] Specifically, the carbon fixing method of the invention comprises the following steps:|[0013] Step one, raw material preparation |[0014] (1) Preparation of slag powder|[0015] Crushing, grinding and screening the steel slag to obtain steel slag powder with the grain size of 100-200 meshes;|[0016] (2) Sintering machine head ash screening |[0017] Screening the sintering machine head ash to remove large-particle impurities to obtain sintering machine head ash with the particle size less than or equal to 100 meshes;|[0018] step two, preparing modified steel slag powder |[0019] Grinding the steel slag powder treated in the first step with sintering machine head ash to obtain modified steel slag powder;|[0020] Step three, roasting the modified steel slag powder and fixing carbon |[0021] And roasting the modified steel slag powder under the condition of introducing CO 2.|[0022] The steel slag used in the invention comprises :CaO36.60～65.85%、SiO22.17～24.94%、Al2O32.91～28.85%、MgO 2.99～7.61%、Fe2O31.74～28.22%、P2O50.05～2.50%, the rest of unavoidable impurities. When the steel slag is directly used for carbon fixation, the carbon fixation capacity is poor due to the poor activity of the steel slag, so that a large amount of CO 2 can not be captured by the steel slag. The constituents of the sinter head ash used include :Fe 10～40%、K2O5～30%、Na2O0.6～5%、MgO0.5～3%、SiO20.3～5%、CaO1～12%、Al2O31～4%、Cl 5～25%, the remainder unavoidable impurities.|[0023] The applicant finds that, through a great deal of research, the sintering machine head ash is doped into steel slag and is subjected to grinding treatment, so that the steel slag can be modified to improve the carbon fixing capability of the steel slag, and the main characteristics are that:|[0024] (1) The sintering machine head ash contains a large amount of metal K, the change of the atomic size of K doping modification positions can cause the contraction or expansion of crystal lattices, the length of a calcium-oxygen bond is changed, the band gap of an energy band is further influenced, and the electronic conductivity and the electronic mobility are changed; |[0025] (2) Invasion of the hetero atom decreases the lattice stability of C 2 S; |[0026] (3) Lattice chemical defects such as doping defects and oxygen vacancy defects are formed, so that ion mobility is improved, the diffusion rate of unreacted Ca 2+ through a CaCO 3 product layer on the surface is accelerated, and gas-solid reaction is promoted. |[0027] Therefore, after the sintering machine head ash is added into the steel slag, the structural stability of C 2 S in the steel slag can be effectively reduced through K modification, the reaction of C 2 S and CO 2 is promoted, and the carbon fixing capacity of the steel slag is improved, so that the purpose of treating waste by waste and recycling resources is realized.|[0028] In a further preferred aspect of the present invention, in the second step, the added mass of the sintering head ash is 1% of the mass of the steel slag powder. The addition amount of the sintering machine head ash is too low, so that the structural stability of C 2 S in the steel slag is difficult to be reduced due to too little K +; too high an amount of the sintering head ash causes excessive K + to block the diffusion of Ca 2+, thereby inhibiting the gas-solid reaction from proceeding, and conversely causing the reduction of the carbon-fixing capacity of the steel slag.|[0029] In the second step, a planetary ball mill is adopted for grinding, the rotating speed is controlled to be 500-800 r/min, and the grinding time is 0.5-1.5 h.|[0030] As a further preferred aspect of the present invention, in the third step, the flow rate of CO 2 to 1000mL/min is introduced.|[0031] As a further preferable mode of the invention, in the third step, the carbon fixing temperature is 650-750 ℃ and the carbon fixing time is 1-2 h. The carbon fixing temperature has an influence on the carbon fixing capacity of the steel slag, and CaCO 3 is generated by utilizing the reaction of CaO and CO 2 in the modified steel slag when the carbon is fixed in the modified steel slag. When the carbon fixing temperature is lower than the requirement of the invention, the carbon fixing reaction may not be carried out or the reaction is incomplete, so that the carbon fixing effect is affected, and when the carbon fixing temperature is higher than the requirement of the invention, caCO 3 is decomposed and CO 2 is generated.|[0032] 3. Advantageous effects|[0033] Compared with the prior art, the invention has the beneficial effects that:|[0034] According to the method for carbon fixation by utilizing the sintering machine head ash to modify the steel slag, the sintering machine head ash is utilized to modify the steel slag, so that the carbon fixation capacity of the steel slag is remarkably improved, the treatment cost is low, and the method is suitable for industrial large-scale application. |[0035] Meanwhile, the sintering machine head ash is used as a steel slag modifier, so that a new thought suitable for recycling treatment is found for the solid waste sintering machine head ash of the steel plant, and the treatment of waste by waste is realized.|INVENTION MODE|Detailed Description|[0036] The invention is further described below in connection with specific embodiments.|[0037] Example 1|[0038] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0039] Step one, raw material preparation |[0040] (1) Preparation of slag powder|[0041] Crushing the steel slag by adopting a jaw crusher, and grinding and screening to obtain steel slag powder with the grain size of 200 meshes.|[0042] (2) Sintering machine head ash screening|[0043] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0044] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities.|[0045] Step two, preparing modified steel slag powder|[0046] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 3% of that of the steel slag powder, the rotating speed of the planetary ball mill is 650r/min, and the grinding time is 1h. And grinding to obtain modified steel slag powder.|[0047] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0048] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0049] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, so that the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass of the crucible is weighed and recorded as m 4, the mass difference before and after the carbon fixation is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1. |[0050] Example 2|[0051] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0052] Step one, raw material preparation |[0053] (1) Preparation of slag powder|[0054] Crushing the steel slag by adopting a jaw crusher, and grinding and sieving to obtain steel slag powder with the grain size of 100-200 meshes.|[0055] (2) Sintering machine head ash screening|[0056] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0057] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities. However, the present embodiment is described by taking the above specific raw material composition as an example, but the specific composition of each raw material is not limited to the present embodiment.|[0058] Step two, preparing modified steel slag powder|[0059] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 1% of that of the steel slag powder, the rotating speed of the planetary ball mill is 500r/min, and the grinding time is 1.5h. And grinding to obtain modified steel slag powder.|[0060] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0061] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0062] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, so that the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass is weighed and recorded as m 4, the mass difference before and after roasting is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1. |[0063] Example 3|[0064] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0065] Step one, raw material preparation |[0066] (1) Preparation of slag powder|[0067] Crushing the steel slag by adopting a jaw crusher, and grinding and sieving to obtain steel slag powder with the grain size of 100-200 meshes.|[0068] (2) Sintering machine head ash screening|[0069] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0070] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities. However, the present embodiment is described by taking the above specific raw material composition as an example, but the specific composition of each raw material is not limited to the present embodiment.|[0071] Step two, preparing modified steel slag powder|[0072] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 10% of that of the steel slag powder, the rotating speed of the planetary ball mill is 800r/min, and the grinding time is 0.5h. And grinding to obtain modified steel slag powder.|[0073] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0074] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0075] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 700 ℃ for roasting, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, so that the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass is weighed and recorded as m 4, the mass difference before and after roasting is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1. |[0076] Example 4|[0077] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0078] Step one, raw material preparation |[0079] (1) Preparation of slag powder|[0080] Crushing the steel slag by adopting a jaw crusher, and grinding and sieving to obtain steel slag powder with the grain size of 100-200 meshes.|[0081] (2) Sintering machine head ash screening|[0082] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0083] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities. However, the present embodiment is described by taking the above specific raw material composition as an example, but the specific composition of each raw material is not limited to the present embodiment.|[0084] Step two, preparing modified steel slag powder|[0085] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 1% of that of the steel slag powder, the rotating speed of the planetary ball mill is 650r/min, and the grinding time is 1h. And grinding to obtain modified steel slag powder.|[0086] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0087] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 650 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0088] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 650 ℃ for roasting, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass is weighed and recorded as m 4, the mass difference before and after roasting is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1.|[0089] Example 5|[0090] The method for carbon fixation by utilizing the ash modified steel slag of the sintering machine head comprises the following specific steps:|[0091] Step one, raw material preparation |[0092] (1) Preparation of slag powder|[0093] Crushing the steel slag by adopting a jaw crusher, and grinding and sieving to obtain steel slag powder with the grain size of 100-200 meshes.|[0094] (2) Sintering machine head ash screening|[0095] And screening the sintering machine head ash by using a 100-mesh screen to remove large-particle impurities, thereby obtaining the sintering machine head ash with the particle size less than or equal to 100 meshes.|[0096] The steel slag and the sintering machine head ash in the embodiment are solid wastes generated by steel plants, wherein the mass percentage of the components of the steel slag is :CaO 47.7%、SiO2 13.3%、Al2O3 3.0%、MgO 6.4%、Fe2O3 24.4%、P2O51.47%,, and the balance is unavoidable impurities; the main chemical components of the sintering machine head ash are as follows by mass percent: fe 25.18%, K18.46%, na8.29%, pb 1.42%, zn 0.28%, cu 0.15%, ca 4.91%, cl 25.18%, and the balance of unavoidable impurities. However, the present embodiment is described by taking the above specific raw material composition as an example, but the specific composition of each raw material is not limited to the present embodiment.|[0097] Step two, preparing modified steel slag powder|[0098] Grinding the steel slag powder and the sintering machine head ash in a planetary ball mill, wherein the mass of the sintering machine head ash is 1% of that of the steel slag powder, the rotating speed of the planetary ball mill is 650r/min, and the grinding time is 1h. And grinding to obtain modified steel slag powder.|[0099] Step three, using modified steel slag powder to carry out carbon fixation and detecting carbon fixation capacity|[0100] (1) 1G of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 1, then the crucible with the modified steel slag powder is put into a muffle furnace at 750 ℃ for roasting, and meanwhile, N 2 with the flow rate of 500mL/min is introduced into the muffle furnace, and the roasting time is 1h. After roasting, naturally cooling the crucible, weighing the mass of the crucible, and marking the mass as m 2, wherein the mass difference before and after roasting is m a, namely m a=m2-m1, and the influence of the self burning loss of the modified steel slag on the mass change before and after carbon fixation of the modified steel slag can be avoided by adopting the operation;|[0101] (2) 1g of modified steel slag powder is put into a corundum crucible, the total mass of the modified steel slag powder and the corundum crucible is weighed by adopting a balance and recorded as m 3, then the crucible with the modified steel slag powder is put into a muffle furnace at 750 ℃ for roasting, and simultaneously CO 2 with the flow rate of 500mL/min is introduced into the muffle furnace, so that the carbon fixation time is 1h. After the carbon fixation is finished, the crucible is naturally cooled, the mass is weighed and recorded as m 4, the mass difference before and after roasting is recorded as m b, namely m b=m3-m4, and the added weight m f=ma+mb,mf after the carbon fixation of the final modified steel slag powder is the mass of fixed CO 2. In this example, after the completion of the experiment, the results of the experiment are recorded as shown in table 1. |[0102] Example 6|[0103] The procedure of this example 1 is basically the same as that of example 1, and the difference between this example 1 is that: the components of the steel slag and the sintering machine head ash adopted are different, and specifically, the steel slag used in the embodiment comprises the following components:|[0104] CaO36.60%、SiO23.14%、Al2O3228.85%、MgO 7.61%、Fe2O32.6%、P2O52.50%, The balance being unavoidable impurities. |[0105] The sinter head ash composition is as follows:|[0106] Fe 40%、K2O30%、Na2O4%、MgO 0.5%、SiO20.3%、CaO12%、Al2O34%、Cl 15%.|[0107] Example 8 |[0108] The procedure of this example 1 is basically the same as that of example 1, and the difference between this example 1 is that: the components of the steel slag and the sintering machine head ash adopted are different, and specifically, the steel slag used in the embodiment comprises the following components:|[0109] CaO36.8%、SiO224.94%、Al2O33.12%、MgO 2.99%、Fe2O328.22%、P2O50.15%, The balance being unavoidable impurities. |[0110] The sinter head ash composition is as follows:|[0111] Fe 20%、K2O28%、Na2O5%、MgO3%、SiO23%、CaO8%、Al2O32%、Cl 5%。|[0112] Comparative example 1 |[0113] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the sintering machine head ash is not added, the crushed and sieved steel slag is directly adopted, the roasting and carbon fixation are carried out under the condition of introducing CO 2, and after the experiment is finished, the experiment result record is shown in table 1.|[0114] Comparative example 2|[0115] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the sintering machine head ash is not added, but the steel slag powder is independently ground, and finally CO 2 is introduced into the ground steel slag for roasting and carbon fixation, and after the experiment is finished, experimental results are recorded as shown in table 1.|[0116] Comparative example 3|[0117] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the sintering machine head ash was added, but the steel slag and the sintering machine head ash were not ground, but were directly mixed, and after the experiment was completed, the experimental results were recorded as shown in table 1.|[0118] Comparative example 4|[0119] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the amounts of the added head ash were varied, specifically, the mass of the added head ash was 0.5% of the mass of the steel slag in this comparative example, and after the experiment was completed, the experimental results were recorded as shown in table 1.|[0120] Comparative example 5|[0121] The method for carbon fixation using steel slag in this comparative example is different from example 1 in that: the amounts of the added head ash were different, specifically, the mass of the added head ash of the sintering machine in this comparative example was 11% of the mass of the steel slag, and after the experiment was completed, the experimental results were recorded as shown in table 1.|[0122] Table 1 carbon sequestration data for each example of the invention and each comparative example|[0123] Numbering devicem1/gm2/gma/gm3/gm4/gmb/gmf/gCarbon fixation ability/g/kgExample 115.22115.2180.00315.22115.2460.0250.02828Example 215.22115.2190.00215.22115.2440.0230.02525Example 315.22115.2160.00515.22115.2430.0220.02727Example 415.22115.2190.00215.22115.2440.0230.02525Example 515.22115.2190.00215.22115.2430.0220.02424Example 615.22115.2170.00415.22115.2430.0220.02626Example 715.22115.2180.00315.22115.2420.0210.02424Example 815.22115.2190.00215.22115.2460.0250.02727Comparative example 115.22115.2180.00315.22115.2290.0080.01111Comparative example 215.22115.2170.00415.22115.2300.0090.01313Comparative example 315.22115.2180.00315.22115.2350.0140.01717Comparative example 415.22115.2190.00215.22115.2310.0100.01212Comparative example 515.22115.2160.00515.22115.2250.0040.0099|[0124] More specifically, although exemplary embodiments of the present invention have been described herein, the present invention is not limited to these embodiments, but includes any and all embodiments that have been modified, omitted, e.g., combined, adapted, and/or substituted between the various embodiments, as would be recognized by those skilled in the art in light of the foregoing detailed description. The limitations in the claims are to be interpreted broadly based on the language employed in the claims and not limited to examples described in the foregoing detailed description or during the prosecution of the application, which examples are to be construed as non-exclusive. Any steps recited in any method or process claims may be executed in any order and are not limited to the order presented in the claims. The scope of the invention should, therefore, be determined only by the appended claims and their legal equivalents, rather than by the descriptions and examples given above.|[0125] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. In case of conflict, the present specification, definitions, will control. Where a rate, pressure, temperature, time, or other value or parameter is expressed as a range, preferred range, or as a range bounded by a list of upper and lower preferred values, this is to be understood as specifically disclosing all ranges formed from any pair of any upper range limit or preferred value and any lower range limit or preferred value, regardless of whether ranges are separately disclosed. For example, a range of 1-50 should be understood to include any number, combination of numbers, or subranges selected from 1、2、3、4、5、6、7、8、9、10、11、12、13、14、15、16、17、18、19、20、21、22、23、24、25、26、27、28、29、30、31、32、33、34、35、36、37、38、39、40、41、42、43、44、45、46、47、48、49 or 50, and all fractional values between the integers described above, e.g., 1.1, 1.2, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8, and 1.9. Regarding sub-ranges, specifically considered are "nested sub-ranges" that extend from any end point within the range. For example, the nested subranges of exemplary ranges 1-50 can include 1-10, 1-20, 1-30, and 1-40 in one direction, or 50-40, 50-30, 50-20, and 50-10 in another direction. Family Number|(110443660)|110443660|Abstract|(CN118267851 A)|The invention discloses a method for carbon sequestration by using sintering machine head ash modified steel slag , and belongs to the technical field of industrial solid waste treatment and environmental protection . According to the carbon sequestration method , steel slag is crushed and screened to obtain steel slag powder , then the steel slag powder and sintering machine head ash are ground according to a certain proportion to obtain modified steel slag powder , and finally the modified steel slag powder is used for direct carbon sequestration . By adopting the technical scheme provided by the invention , the carbon sequestration capability of the steel slag can be obviously improved , the purpose of capturing CO2 by using the steel slag is effectively realized , and meanwhile , a good way is provided for utilizing the steel slag and the sintering machine head ash . |CPC codes|(CN118267851 A)|B01D - 053/62 |B01D - 053/82 |B01D - 2251/302 |B01D - 2251/402 |B01D - 2251/404 |B01D - 2251/602 |IPC codes|(CN118267851 A)|B01D - 053/62 |B01D - 053/82 |Title|(CN118267851 A)|Method for carbon sequestration by using sintering machine head ash modified steel slag | Environmental technology B01D-053/62|B01D-053/82|B01D-2251/302|B01D-2251/402|B01D-2251/404|B01D-2251/602|B09B-003/00|B09B-003/35|B09B-003/38|B09B-003/40|B09B-2101/55 B01D-053/62|B01D-053/82|B01D-2251/302|B01D-2251/402|B01D-2251/404|B01D-2251/602|B09B-003/00|B09B-003/35|B09B-003/38|B09B-003/40|B09B-2101/55 B01D-053/62|B01D-053/82|B09B-003/00|B09B-003/35|B09B-003/38|B09B-003/40|B09B-101/55 B01D-053/62|B01D-053/82|B09B-003/00|B09B-003/35|B09B-003/38|B09B-003/40|B09B-101/55 PENDING (CN118267851)|PENDING ALIVE (CN118267851)|ALIVE (CN118267851)|LEGAL DETAILS FOR CN118267851|Actual or expected expiration date=2044-04-30|Legal state=ALIVE|Status=PENDING|Event publication date=2024-04-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202410538454|Application date=2024-04-30|Standardized application number=2024CN-0538454|Event publication date=2024-07-02|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN118267851|Publication stage code=A|Publication date=2024-07-02|Standardized publication number=CN118267851|Event publication date=2024-07-02|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-07-19|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN118267851)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoS48LdyoAp9glfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=9MIjnBEAO56QHB7%252FyzhGH5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN118267851)|CN (CN118267851)|NAME=ANHUI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN118267851)|NAME=SHANG XIANFANG;WEN PARTNERS P.C. , REG=34134 (CN118267851)|NAME=LONG HONGMING|NAME=FAN CHUNLONG|NAME=WEI RUFEI|NAME=SUN RONG|NAME=DING RAN|NAME=ZHANG HAO|NAME=DI ZHANXIA 0 1 Titre: (CN118267851)|Method for carbon sequestration by using sintering machine head ash modified steel slag Résumé: (CN118267851)|The invention discloses a method for carbon sequestration by using sintering machine head ash modified steel slag, and belongs to the technical field of industrial solid waste treatment and environmental protection. According to the carbon sequestration method, steel slag is crushed and screened to obtain steel slag powder, then the steel slag powder and sintering machine head ash are ground according to a certain proportion to obtain modified steel slag powder, and finally the modified steel slag powder is used for direct carbon sequestration. By adopting the technical scheme provided by the invention, the carbon sequestration capability of the steel slag can be obviously improved, the purpose of capturing CO2 by using the steel slag is effectively realized, and meanwhile, a good way is provided for utilizing the steel slag and the sintering machine head ash. 9 Abstract gpt-4o-mini no The focus is on carbon sequestration using modified steel slag, which does not involve the accelerated weathering of silicate or alkaline minerals for CO₂ capture.
16 CN201510076568 CN201510076568 CN104641756 69443585 CN104641756 A 2015-05-27 [CN104641756] 2015-02-12 2015-02-12 2015-05-27 (CN104641756)|2017-09-26 (CN104641756)|Method for increasing carbon sequestration capacity of soil of mining area (CN104641756)|The invention relates to a method for increasing the carbon sequestration capacity of soil of a mining area. The method comprises the steps: (1) ridging the soil; (2) during ridging, burying crushed straws into ridge furrows and applying urea and a straw decomposition agent; (3) composting from the last third of March to the first third of April in a next year; (4) before sowing, fertilizing and then planting green manure crops; (5) from the last third of September to the first third of October, ridging, spraying crushed crop straws into new ridge furrows, and applying urea and the straw decomposition agent; (6) composting decomposed manure from the last third of March to the first third of April in a third year; (7) before sowing, fertilizing and then planting maize; (8) from the last third of September to the first third of October, ridging, crushing maize straws, spraying the crushed maize straws into ridge furrows, and applying urea and the straw decomposition agent; (9) repeating the steps (6) to (8) in a fourth year. The method has the following beneficial effects that the carbon sequestration capacity of the soil of the mining area can be rapidly increased; solid wastes of the mining area can be effectively utilized; the consumption of chemical fertilizers is lowered, and the fertility of the soil is improved while the carbon sequestration capacity of the soil is increased; the economic cost is low, and the operability is strong. INSTITUTE OF AGRICULTURAL ENVIRONMENT & RESOURCE SHANXI ACADEMY OF AGRICULTURAL SCIENCES (CN104641756)|INSTITUTE OF AGRICULTURAL ENVIRONMENT AND RESOURCE, SHANXI ACADEMY OF AGRICULTURAL SCIENCES ([CN]) ZHANG QIANG|JIN DONGSHENG|GAO CHUNHUA|LI JIANHUA|LU CHAODONG|DONG YUNZHONG|LU JINJING (CN104641756)|ZHANG QIANG|JIN DONGSHENG|GAO CHUNHUA|LI JIANHUA|LU CHAODONG|DONG YUNZHONG|LU JINJING (CN104641756)|GUO GUANHOU;BEIJING SUTHINK PATENT AGENCY FIRM (ORDINARY PARTNERSHIP) (CN104641756)|4. the method has the advantages of low economic cost and strong operability.| (CN104641756)|1. A method for improving the carbon sequestration capacity of the soil in a mining area is characterized by comprising the following steps:(1) ridging on the reclaimed soil in the mining area;(2) crushing corn straws, wherein the length of the crushed straws is not more than 10cm, burying the crushed straws into furrows during ridging, and applying 5-10 kg of urea and 2-4 kg of straw decomposition agent per mu;(3) mixing 4-6 parts of farmyard manure, 2-4 parts of biological carbon and 1-2 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days of the next year, and carrying out stack retting fermentation for 15-20 days to completely decompose the fertilizer;(4) before sowing, uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows, turning over, and then planting green manure crops in the furrows;(5) after harvesting crops, turning soil on the ridges into furrows to form new ridges, crushing the harvested crop straws, wherein the length of the crushed straws is not more than 10cm, scattering the crushed straws into the new furrows, and applying 5-10 kg of urea and 2-4 kg of straw decomposing agents to each mu;(6) mixing 4-6 parts of farmyard manure, 2-4 parts of biological carbon and 1-2 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days of the third year, and carrying out stack retting fermentation for 15-20 days to completely decompose the fertilizer;(7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal mass into furrows before sowing, turning over, and then planting corn in the furrows;(8) after harvesting corns in the last ten days of 9 months to 10 months, turning soil on the ridges into furrows to form new ridges, crushing and scattering corn straws into the new furrows, wherein the length of the crushed straws is not more than 10cm, and 5-10 kg of urea and 2-4 kg of straw decomposition agent are applied to each mu;(9) and (5) repeating the steps (6) to (8) in the fourth year.| (CN104641756)|The invention relates to a method for increasing the carbon sequestration capacity of soil of a mining area.|The purpose of the invention is as follows: the invention aims at solving the problems in the prior art, namely the invention discloses a method for improving the carbon sequestration capacity of the soil in a mining area.| (CN104641756)|MINING AREA(100,34)|CARBON SEQUESTRATION(100,31)|CARBON SEQUESTRATION CAPACITY(100,31)|SOIL CARBON SEQUESTRATION CAPACITY(100,25)|MINING AREA SOIL(100,3)|CRUSHED STRAW(99,18)|STRAW DECOMPOSITION(86,18)|COMPOSTING DECOMPOSED MANURE(77,1)|FERTILIZER COMPOUND(75,50)|HARVESTED CROP STRAW(75,2)|DECOMPOSE FERTILIZER(73,5)|RIDGE FURROW(72,3)|TETRASTRONG STRAW DECOMPOSING INOCULANT(72,1)|BURYING CRUSHED STRAW(65,1)|CRUSHED MAIZE STRAW(65,1)|CRUSHING MAIZE STRAW(64,1)|DECOMPOSED FERTILIZER(63,10)|PLANT ASH(60,23)|GREEN MANURE CROP(59,5)|CRUSHED CROP STRAW(58,1)|FURROW(52,53)|FARMYARD MANURE(52,22)|STRAW DECOMPOSING(49,4)|CRUSHED STRAW LENGTH(48,10)|HARVESTED CROP(48,2)|HARVESTING CORN(46,2)|YEAR EARLY TEN DAY(46,2)|CORN PLANTING(45,2)|LATE TEN DAY(44,8)|PLANTING MAIZE(41,1)|LAND RECLAMATION(40,5)|EARLY TEN DAY(39,8)|CRUSHING CORN STRAW(39,4)|CHICKEN DUNG(37,1)|RIDGE(36,20)|SCATTERING CORN STRAW(36,5)|OPERABILITY(36,2)|TURNING SOIL(35,9)|CARBONYLDIAMIDE(34,18)|SHEEP DUNG(34,1)|PIG DUNG(32,1)|FIREWOOD COMBUSTION(31,4)|SOWING(30,12)|FERMENTATION(28,8)|TOTAL FERTILIZING(25,10)|RIDGE SPACING(25,1)|POTASSIUM COMPOUND FERTILIZER(24,10)|ASH SUBSTANCE(23,2)|CHEMICAL FERTILIZER CONSUMPTION(23,1)|PHOSPHORUS PENTOXIDE(19,10)|FARMYARD MANURE DECOMPOSITION(19,5)|CRUSHING(18,5)|ECONOMIC COST(17,2)|STRAW DECAY(16,5)|BIOCHAR(14,9)|RIDGE BACK RIDGE HEIGHT(14,5)|ZHONGBANG BIOTECHNOLOGY(14,3)|HARVESTED HAIR VETCH STRAW(14,1)|COW DUNG(13,2)|EQUAL MASS(13,2)|GROUND(13,2)|FARM MANURE(12,3)|HARVESTED MISCANTHUS STRAW(12,1)|EQUAL QUALITY(11,8)|HOG MANURE(11,3)|PLANTING CORN(11,3)|HARVESTED ALFALFA STRAW(11,1)|LATE MONTH(10,4)|RIDGING MACHINE(9,3)|SHEEP MANURE(9,2)|POTASSIUM OXIDE(8,10)|KEY METALLURGICAL MINE(8,1)|PLANTING CHINESE SILVERGRASS(8,1)|NEXT YEAR EARLY MONTH(7,3)|PLANTING ALFALFA(7,1)|PLANTING HAIRY VETCH(7,1)|RIDGE DISTANCE(6,4)| (CN104641756)|1. A method for improving the carbon sequestration capacity of the soil in a mining area is characterized by comprising the following steps:|(1) ridging on the reclaimed soil in the mining area;|(2) crushing corn straws, wherein the length of the crushed straws is not more than 10cm, burying the crushed straws into furrows during ridging, and applying 5-10 kg of urea and 2-4 kg of straw decomposition agent per mu;|(3) mixing 4-6 parts of farmyard manure, 2-4 parts of biological carbon and 1-2 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days of the next year, and carrying out stack retting fermentation for 15-20 days to completely decompose the fertilizer;|(4) before sowing, uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows, turning over, and then planting green manure crops in the furrows;|(5) after harvesting crops, turning soil on the ridges into furrows to form new ridges, crushing the harvested crop straws, wherein the length of the crushed straws is not more than 10cm, scattering the crushed straws into the new furrows, and applying 5-10 kg of urea and 2-4 kg of straw decomposing agents to each mu;|(6) mixing 4-6 parts of farmyard manure, 2-4 parts of biological carbon and 1-2 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days of the third year, and carrying out stack retting fermentation for 15-20 days to completely decompose the fertilizer;|(7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal mass into furrows before sowing, turning over, and then planting corn in the furrows;|(8) after harvesting corns in the last ten days of 9 months to 10 months, turning soil on the ridges into furrows to form new ridges, crushing and scattering corn straws into the new furrows, wherein the length of the crushed straws is not more than 10cm, and 5-10 kg of urea and 2-4 kg of straw decomposition agent are applied to each mu;|(9) and (5) repeating the steps (6) to (8) in the fourth year.|2. The method for improving the carbon sequestration capacity of the soil in the mining area according to claim 1, wherein in the step (1), the ridge height of the ridge back is 10-15 cm, the bottom width of the ridge back is 50-60 cm, and the ridge spacing is 30-40 cm.|3. The method for improving the carbon sequestration capacity of the soil in the mining area according to claim 1, wherein the straw-decomposing inoculant in the step (2), the step (5) and the step (8) is a tetrastrong straw-decomposing inoculant.|4. The method for improving the carbon sequestration capacity of the soil in the mining area according to claim 1, wherein the farmyard manure in the step (3) is one or a mixture of more of cow dung, chicken dung, pig dung and sheep dung, the biochar in the step (3) is produced by using straws, and the plant ash in the step (3) is ash substances remained after the combustion of firewood.|5. The method of claim 1, wherein the green manure crops in step (4) comprise vetch, alfalfa and miscanthus.|6. The method for improving the carbon sequestration capacity of the soil in the mining area according to claim 1, wherein the total fertilizing amount in the step (4) is 30-40 kg/mu.|7. The method for improving the carbon sequestration capacity of the soil in the mining area according to claim 1, wherein the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|8. The method for improving the carbon sequestration capacity of the soil in the mining area according to claim 1, wherein the total fertilizing amount in the step (7) is 40-50 kg/mu.|9. The method for improving the carbon sequestration capacity of the soil in the mining area according to claim 1, wherein the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide. (CN104641756)|TECHNICAL FIELD|[0002] The invention belongs to the field of soil improvement, and particularly relates to a method for improving the carbon sequestration capacity of mine soil.|BACKGROUND ART|[0004] The mine is not only a production base of raw materials and energy, but also often becomes a main pollution source, the mine not only occupies a large area (for example, the occupied area of the key metallurgical mine in China is 6.5 ten thousand square meters, wherein the occupied areas of an open stope, a dumping site and a tailing site are about 70 percent), but also has large-scale human activities, so that the underground water level in the mine area is greatly reduced, and the carbon sequestration capacity of an overground ecological system is greatly reduced.|DISCLOSURE|[0005] Disclosure of Invention|[0006] The purpose of the invention is as follows: the invention aims at solving the problems in the prior art, namely the invention discloses a method for improving the carbon sequestration capacity of the soil in a mining area.|[0007] The technical scheme is as follows: a method for improving the carbon sequestration capacity of the soil in a mining area comprises the following steps:|[0008] (1) ridging on the reclaimed soil in the mining area;|[0009] (2) crushing corn straws, wherein the length of the crushed straws is not more than 10cm, burying the crushed straws into furrows during ridging, and applying 5-10 kg of urea and 2-4 kg of straw decomposition agent per mu;|[0010] (3) mixing 4-6 parts of farmyard manure, 2-4 parts of biological carbon and 1-2 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days of the next year, and carrying out stack retting fermentation for 15-20 days to completely decompose the fertilizer;|[0011] (4) before sowing, uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows, turning over, and then planting green manure crops in the furrows;|[0012] (5) after harvesting crops, turning soil on the ridges into furrows to form new ridges, crushing the harvested crop straws, wherein the length of the crushed straws is not more than 10cm, scattering the crushed straws into the new furrows, and applying 5-10 kg of urea and 2-4 kg of straw decomposing agents to each mu;|[0013] (6) mixing 4-6 parts of farmyard manure, 2-4 parts of biological carbon and 1-2 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days of the third year, and carrying out stack retting fermentation for 15-20 days to completely decompose the fertilizer;|[0014] (7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal mass into furrows before sowing, turning over, and then planting corn in the furrows;|[0015] (8) after harvesting corns in the last ten days of 9 months to 10 months, turning soil on the ridges into furrows to form new ridges, crushing and scattering corn straws into the new furrows, wherein the length of the crushed straws is not more than 10cm, and 5-10 kg of urea and 2-4 kg of straw decomposition agent are applied to each mu;|[0016] (9) and (5) repeating the steps (6) to (8) in the fourth year.|[0017] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: in the step (1), the ridge height of the ridge back is 10-15 cm, the bottom width of the ridge back is 50-60 cm, and the ridge distance is 30-40 cm.|[0018] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: the straw decomposing inoculant in the step (2), the step (5) and the step (8) is a four-strong straw decomposing inoculant.|[0019] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: and (3) the farmyard manure is one or a mixture of more of cow manure, chicken manure, pig manure and sheep manure, the biochar is produced by utilizing straws in the step (3), and the plant ash is ash substances remained after firewood is combusted in the step (3).|[0020] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: the green manure crops in the step (4) comprise vetch, alfalfa and Chinese silvergrass.|[0021] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: and (4) the total fertilizing amount in the step (4) is 30-40 kilograms per mu.|[0022] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0023] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: in the step (7), the total fertilizing amount is 40-50 kg/mu.|[0024] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0025] Has the advantages that: the method for improving the carbon sequestration capacity of the soil in the mining area disclosed by the invention has the following beneficial effects:|[0026] 1. the carbon sequestration capacity of the soil in the mining area can be rapidly improved, and the problems of low carbon content, weak carbon sequestration capacity and rapid decomposition of soil carbon in the mining area are solved;|[0027] 2. the solid wastes in the mining area can be effectively utilized, the wastes are changed into valuable, the resource utilization rate is improved, and the development of circular economy is promoted;|[0028] 3. the application amount of the fertilizer can be reduced, the carbon sequestration capacity of the soil is improved, the soil fertility is improved, the physical and chemical properties of the soil are improved, and the land productivity is improved;|[0029] 4. the method has the advantages of low economic cost and strong operability.|INVENTION MODE|[0030] The specific implementation mode is as follows:|[0031] the following describes in detail specific embodiments of the present invention.|INVENTION MODE|[0032] Detailed description of the preferred embodiment 1|[0033] A method for improving the carbon sequestration capacity of the soil in a mining area comprises the following steps:|[0034] (1) ridging the reclaimed soil in the mining area by using a ridging machine to form ridge backs and furrows;|[0035] (2) crushing corn straws, wherein the length of the crushed straws is not more than 10cm, burying the crushed straws into furrows during ridging, applying 5 kg of urea and 2 kg of straw decomposition agent per mu, and accelerating the decomposition of the straws by using water accumulated in the furrows;|[0036] (3) mixing 4 parts of farmyard manure, 2 parts of biochar and 1 part of plant ash uniformly according to a proportion from 3 late months to 4 early months of the next year, and carrying out stack retting fermentation for 15 days to completely decompose the farmyard manure;|[0037] (4) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows before sowing (5 last ten days), turning over, and then planting hairy vetch in the furrows;|[0038] (5) in the ten days from the next month of 9 months to the last month of 10 months, after the hair vetch is harvested, turning soil on the ridges into furrows to form new ridges, changing the original ridge back position into furrows, then crushing the harvested hair vetch straws, enabling the length of the crushed straws not to exceed 10cm, scattering the crushed straws into the new furrows, applying 5 kg of urea and 2 kg of straw decomposition agent to each mu, accelerating the decomposition of the straws by utilizing the water accumulated in the furrows,|[0039] (6) mixing 4 parts of farmyard manure, 2 parts of biochar and 1 part of plant ash uniformly according to a proportion from 3 late months to 4 early months in the third year, and carrying out stack retting fermentation for 15 days to completely decompose the farmyard manure;|[0040] (7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal quality into furrows before sowing (4 late ten days to 5 early ten days in month), ploughing, and then planting corns in the furrows;|[0041] (8) in ten days from the next month of 9 months to the last month of 10 months, after the corn is harvested, turning soil on the ridges into furrows to form new ridges, changing the positions of the backs of the original ridges into furrows, then crushing and scattering corn straws into the new furrows, applying 5 kilograms of urea and 2 kilograms of straw decomposing agents to each mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0042] (9) and (5) repeating the steps (6) to (8) in the fourth year.|[0043] In the embodiment, in the step (1), the ridge height of the ridge back is 10cm, the bottom width of the ridge back is 50cm, and the ridge distance is 30 cm.|[0044] In this embodiment, the straw-decomposing inoculant in the steps (2), (5) and (8) is a four-strong straw-decomposing inoculant. It is produced by Zhongbang biotechnology, Inc. in Hebei.|[0045] In this embodiment, the farm manure in step (3) is cow dung, the biochar in step (3) is produced by using straws, and the plant ash in step (3) is ash material remaining after the combustion of firewood.|[0046] In this example, the total fertilizing amount in the step (4) is 30 kg/mu.|[0047] In the embodiment, the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0048] In this example, the total fertilizing amount in step (7) is 40 kg/mu.|[0049] In the embodiment, the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|INVENTION MODE|[0050] Specific example 2|[0051] A method for improving the carbon sequestration capacity of the soil in a mining area comprises the following steps:|[0052] (1) ridging the reclaimed soil in the mining area by using a ridging machine to form ridge backs and furrows;|[0053] (2) crushing corn straws, wherein the length of the crushed straws is not more than 10cm, burying the crushed straws into furrows during ridging, applying 10 kilograms of urea and 4 kilograms of straw decomposition agents per mu, and accelerating the decomposition of the straws by utilizing water accumulated in the furrows;|[0054] (3) mixing 6 parts of farmyard manure, 4 parts of biochar and 2 parts of plant ash uniformly according to a proportion from 3 late months to 4 early months of the next year, and carrying out stack retting fermentation for 20 days to completely decompose the farmyard manure;|[0055] (4) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows before sowing (5 last ten days), turning over, and then planting alfalfa in the furrows;|[0056] (5) in the last ten days of 9 months to 10 months, after the alfalfa is harvested, turning soil on the ridges into furrows to form new ridges, changing the original ridge back position into the furrows, then crushing the harvested alfalfa straws, enabling the length of the crushed straws not to exceed 10cm, scattering the crushed straws into the new furrows, applying 10 kg of urea and 4 kg of straw decomposition agent per mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0057] (6) mixing 6 parts of farmyard manure, 4 parts of biological carbon and 2 parts of plant ash uniformly according to a proportion from 3 late to 4 early days in spring of the third year, and composting and fermenting for 20 days to completely decompose the farmyard manure;|[0058] (7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal quality into furrows before sowing (4 late ten days to 5 early ten days in month), ploughing, and then planting corns in the furrows;|[0059] (8) in ten days from the next month of 9 months to the last month of 10 months, after the corn is harvested, turning soil on the ridges into furrows to form new ridges, changing the positions of the backs of the original ridges into furrows, then crushing and scattering corn straws into the new furrows, applying 10 kilograms of urea and 4 kilograms of straw decomposing agents to each mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0060] (9) and (5) repeating the steps (6) to (8) in the fourth year.|[0061] In the embodiment, in the step (1), the ridge height of the ridge back is 15cm, the bottom width of the ridge back is 60cm, and the ridge distance is 40 cm.|[0062] In this embodiment, the straw-decomposing inoculant in the steps (2), (5) and (8) is a four-strong straw-decomposing inoculant. It is produced by Zhongbang biotechnology, Inc. in Hebei.|[0063] In this embodiment, the farm manure in step (3) is a mixture of cow manure, chicken manure, pig manure, and sheep manure, the biochar in step (3) is produced by using straws, and the plant ash in step (3) is ash material remaining after combustion of firewood.|[0064] In this example, the total fertilizing amount in the step (4) is 40 kg/mu.|[0065] In the embodiment, the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0066] In this example, the total fertilizing amount in step (7) is 50 kg/mu.|[0067] In the embodiment, the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|INVENTION MODE|[0068] Specific example 3|[0069] A method for improving the carbon sequestration capacity of the soil in a mining area comprises the following steps:|[0070] (1) ridging the reclaimed soil in the mining area by using a ridging machine to form ridge backs and furrows;|[0071] (2) crushing the corn straws, wherein the length of the straws is not more than 10cm, burying the straws in furrows during ridging, applying 7 kg of urea and 3 kg of straw decomposition agent per mu, and accelerating the decomposition of the straws by using water accumulated in the furrows;|[0072] (3) mixing 5 parts of farmyard manure, 3 parts of biochar and 1.5 parts of plant ash uniformly according to a proportion from 3 late months to 4 early months of the next year, and carrying out stack retting fermentation for 18 days to completely decompose the farmyard manure;|[0073] (4) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows before sowing (5 last ten days), turning over, and then planting Chinese silvergrass in the furrows;|[0074] (5) in ten days from the next month of 9 months to the last month of 10 months, after the miscanthus is harvested, turning the soil on the ridge into furrows to form new ridges, changing the original ridge back position into the furrows, then crushing the harvested miscanthus straws, wherein the length of the straws is not more than 10cm, scattering the straws into the new furrows, applying 8 kg of urea and 3 kg of straw decomposition agent per mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0075] (6) mixing 5 parts of farmyard manure, 3 parts of biological carbon and 1.5 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days in spring of the third year, and composting and fermenting for 18 days to completely decompose the fertilizer;|[0076] (7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal quality into furrows before sowing (4 late ten days to 5 early ten days in month), ploughing, and then planting corns in the furrows;|[0077] (8) in ten days from the next month of 9 months to the last month of 10 months, after the corn is harvested, turning soil on the ridges into furrows to form new ridges, changing the positions of the backs of the original ridges into furrows, then crushing and scattering corn straws into the new furrows, applying 8 kilograms of urea and 3 kilograms of straw decomposition agents to each mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0078] (9) and (5) repeating the steps (6) to (8) in the fourth year.|[0079] In the embodiment, in the step (1), the ridge height of the ridge back is 13cm, the bottom width of the ridge back is 55cm, and the ridge distance is 35 cm.|[0080] In this embodiment, the straw-decomposing inoculant in the steps (2), (5) and (8) is a four-strong straw-decomposing inoculant. It is produced by Zhongbang biotechnology, Inc. in Hebei.|[0081] In this embodiment, the farm manure in step (3) is pig manure, the biochar in step (3) is produced by using straws, and the plant ash in step (3) is ash material remaining after the combustion of firewood.|[0082] In this example, the total fertilizing amount in the step (4) is 35 kg/mu.|[0083] In the embodiment, the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0084] In this example, the total fertilizing amount in the step (7) is 45 kg/mu.|[0085] In the embodiment, the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0086] The embodiments of the present invention have been described in detail. However, the present invention is not limited to the above-described embodiments, and various changes can be made within the knowledge of those skilled in the art without departing from the spirit of the present invention. (CN104641756)|TECHNICAL FIELD|[0002] The invention belongs to the field of soil improvement, and particularly relates to a method for improving the carbon sequestration capacity of mine soil.|BACKGROUND ART|[0004] The mine is not only a production base of raw materials and energy, but also often becomes a main pollution source, the mine not only occupies a large area (for example, the occupied area of the key metallurgical mine in China is 6.5 ten thousand square meters, wherein the occupied areas of an open stope, a dumping site and a tailing site are about 70 percent), but also has large-scale human activities, so that the underground water level in the mine area is greatly reduced, and the carbon sequestration capacity of an overground ecological system is greatly reduced.|DISCLOSURE|[0005] Disclosure of Invention|[0006] The purpose of the invention is as follows: the invention aims at solving the problems in the prior art, namely the invention discloses a method for improving the carbon sequestration capacity of the soil in a mining area.|[0007] The technical scheme is as follows: a method for improving the carbon sequestration capacity of the soil in a mining area comprises the following steps:|[0008] (1) ridging on the reclaimed soil in the mining area;|[0009] (2) crushing corn straws, wherein the length of the crushed straws is not more than 10cm, burying the crushed straws into furrows during ridging, and applying 5-10 kg of urea and 2-4 kg of straw decomposition agent per mu;|[0010] (3) mixing 4-6 parts of farmyard manure, 2-4 parts of biological carbon and 1-2 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days of the next year, and carrying out stack retting fermentation for 15-20 days to completely decompose the fertilizer;|[0011] (4) before sowing, uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows, turning over, and then planting green manure crops in the furrows;|[0012] (5) after harvesting crops, turning soil on the ridges into furrows to form new ridges, crushing the harvested crop straws, wherein the length of the crushed straws is not more than 10cm, scattering the crushed straws into the new furrows, and applying 5-10 kg of urea and 2-4 kg of straw decomposing agents to each mu;|[0013] (6) mixing 4-6 parts of farmyard manure, 2-4 parts of biological carbon and 1-2 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days of the third year, and carrying out stack retting fermentation for 15-20 days to completely decompose the fertilizer;|[0014] (7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal mass into furrows before sowing, turning over, and then planting corn in the furrows;|[0015] (8) after harvesting corns in the last ten days of 9 months to 10 months, turning soil on the ridges into furrows to form new ridges, crushing and scattering corn straws into the new furrows, wherein the length of the crushed straws is not more than 10cm, and 5-10 kg of urea and 2-4 kg of straw decomposition agent are applied to each mu;|[0016] (9) and (5) repeating the steps (6) to (8) in the fourth year.|[0017] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: in the step (1), the ridge height of the ridge back is 10-15 cm, the bottom width of the ridge back is 50-60 cm, and the ridge distance is 30-40 cm.|[0018] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: the straw decomposing inoculant in the step (2), the step (5) and the step (8) is a four-strong straw decomposing inoculant.|[0019] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: and (3) the farmyard manure is one or a mixture of more of cow manure, chicken manure, pig manure and sheep manure, the biochar is produced by utilizing straws in the step (3), and the plant ash is ash substances remained after firewood is combusted in the step (3).|[0020] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: the green manure crops in the step (4) comprise vetch, alfalfa and Chinese silvergrass.|[0021] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: and (4) the total fertilizing amount in the step (4) is 30-40 kilograms per mu.|[0022] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0023] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: in the step (7), the total fertilizing amount is 40-50 kg/mu.|[0024] As a preferred scheme of the method for improving the carbon sequestration capacity of the soil in the mining area, the method comprises the following steps: the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0025] Has the advantages that: the method for improving the carbon sequestration capacity of the soil in the mining area disclosed by the invention has the following beneficial effects:|[0026] 1. the carbon sequestration capacity of the soil in the mining area can be rapidly improved, and the problems of low carbon content, weak carbon sequestration capacity and rapid decomposition of soil carbon in the mining area are solved;|[0027] 2. the solid wastes in the mining area can be effectively utilized, the wastes are changed into valuable, the resource utilization rate is improved, and the development of circular economy is promoted;|[0028] 3. the application amount of the fertilizer can be reduced, the carbon sequestration capacity of the soil is improved, the soil fertility is improved, the physical and chemical properties of the soil are improved, and the land productivity is improved;|[0029] 4. the method has the advantages of low economic cost and strong operability.|INVENTION MODE|[0030] The specific implementation mode is as follows:|[0031] the following describes in detail specific embodiments of the present invention.|INVENTION MODE|[0032] Detailed description of the preferred embodiment 1|[0033] A method for improving the carbon sequestration capacity of the soil in a mining area comprises the following steps:|[0034] (1) ridging the reclaimed soil in the mining area by using a ridging machine to form ridge backs and furrows;|[0035] (2) crushing corn straws, wherein the length of the crushed straws is not more than 10cm, burying the crushed straws into furrows during ridging, applying 5 kg of urea and 2 kg of straw decomposition agent per mu, and accelerating the decomposition of the straws by using water accumulated in the furrows;|[0036] (3) mixing 4 parts of farmyard manure, 2 parts of biochar and 1 part of plant ash uniformly according to a proportion from 3 late months to 4 early months of the next year, and carrying out stack retting fermentation for 15 days to completely decompose the farmyard manure;|[0037] (4) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows before sowing (5 last ten days), turning over, and then planting hairy vetch in the furrows;|[0038] (5) in the ten days from the next month of 9 months to the last month of 10 months, after the hair vetch is harvested, turning soil on the ridges into furrows to form new ridges, changing the original ridge back position into furrows, then crushing the harvested hair vetch straws, enabling the length of the crushed straws not to exceed 10cm, scattering the crushed straws into the new furrows, applying 5 kg of urea and 2 kg of straw decomposition agent to each mu, accelerating the decomposition of the straws by utilizing the water accumulated in the furrows,|[0039] (6) mixing 4 parts of farmyard manure, 2 parts of biochar and 1 part of plant ash uniformly according to a proportion from 3 late months to 4 early months in the third year, and carrying out stack retting fermentation for 15 days to completely decompose the farmyard manure;|[0040] (7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal quality into furrows before sowing (4 late ten days to 5 early ten days in month), ploughing, and then planting corns in the furrows;|[0041] (8) in ten days from the next month of 9 months to the last month of 10 months, after the corn is harvested, turning soil on the ridges into furrows to form new ridges, changing the positions of the backs of the original ridges into furrows, then crushing and scattering corn straws into the new furrows, applying 5 kilograms of urea and 2 kilograms of straw decomposing agents to each mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0042] (9) and (5) repeating the steps (6) to (8) in the fourth year.|[0043] In the embodiment, in the step (1), the ridge height of the ridge back is 10cm, the bottom width of the ridge back is 50cm, and the ridge distance is 30 cm.|[0044] In this embodiment, the straw-decomposing inoculant in the steps (2), (5) and (8) is a four-strong straw-decomposing inoculant. It is produced by Zhongbang biotechnology, Inc. in Hebei.|[0045] In this embodiment, the farm manure in step (3) is cow dung, the biochar in step (3) is produced by using straws, and the plant ash in step (3) is ash material remaining after the combustion of firewood.|[0046] In this example, the total fertilizing amount in the step (4) is 30 kg/mu.|[0047] In the embodiment, the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0048] In this example, the total fertilizing amount in step (7) is 40 kg/mu.|[0049] In the embodiment, the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|INVENTION MODE|[0050] Specific example 2|[0051] A method for improving the carbon sequestration capacity of the soil in a mining area comprises the following steps:|[0052] (1) ridging the reclaimed soil in the mining area by using a ridging machine to form ridge backs and furrows;|[0053] (2) crushing corn straws, wherein the length of the crushed straws is not more than 10cm, burying the crushed straws into furrows during ridging, applying 10 kilograms of urea and 4 kilograms of straw decomposition agents per mu, and accelerating the decomposition of the straws by utilizing water accumulated in the furrows;|[0054] (3) mixing 6 parts of farmyard manure, 4 parts of biochar and 2 parts of plant ash uniformly according to a proportion from 3 late months to 4 early months of the next year, and carrying out stack retting fermentation for 20 days to completely decompose the farmyard manure;|[0055] (4) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows before sowing (5 last ten days), turning over, and then planting alfalfa in the furrows;|[0056] (5) in the last ten days of 9 months to 10 months, after the alfalfa is harvested, turning soil on the ridges into furrows to form new ridges, changing the original ridge back position into the furrows, then crushing the harvested alfalfa straws, enabling the length of the crushed straws not to exceed 10cm, scattering the crushed straws into the new furrows, applying 10 kg of urea and 4 kg of straw decomposition agent per mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0057] (6) mixing 6 parts of farmyard manure, 4 parts of biological carbon and 2 parts of plant ash uniformly according to a proportion from 3 late to 4 early days in spring of the third year, and composting and fermenting for 20 days to completely decompose the farmyard manure;|[0058] (7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal quality into furrows before sowing (4 late ten days to 5 early ten days in month), ploughing, and then planting corns in the furrows;|[0059] (8) in ten days from the next month of 9 months to the last month of 10 months, after the corn is harvested, turning soil on the ridges into furrows to form new ridges, changing the positions of the backs of the original ridges into furrows, then crushing and scattering corn straws into the new furrows, applying 10 kilograms of urea and 4 kilograms of straw decomposing agents to each mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0060] (9) and (5) repeating the steps (6) to (8) in the fourth year.|[0061] In the embodiment, in the step (1), the ridge height of the ridge back is 15cm, the bottom width of the ridge back is 60cm, and the ridge distance is 40 cm.|[0062] In this embodiment, the straw-decomposing inoculant in the steps (2), (5) and (8) is a four-strong straw-decomposing inoculant. It is produced by Zhongbang biotechnology, Inc. in Hebei.|[0063] In this embodiment, the farm manure in step (3) is a mixture of cow manure, chicken manure, pig manure, and sheep manure, the biochar in step (3) is produced by using straws, and the plant ash in step (3) is ash material remaining after combustion of firewood.|[0064] In this example, the total fertilizing amount in the step (4) is 40 kg/mu.|[0065] In the embodiment, the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0066] In this example, the total fertilizing amount in step (7) is 50 kg/mu.|[0067] In the embodiment, the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|INVENTION MODE|[0068] Specific example 3|[0069] A method for improving the carbon sequestration capacity of the soil in a mining area comprises the following steps:|[0070] (1) ridging the reclaimed soil in the mining area by using a ridging machine to form ridge backs and furrows;|[0071] (2) crushing the corn straws, wherein the length of the straws is not more than 10cm, burying the straws in furrows during ridging, applying 7 kg of urea and 3 kg of straw decomposition agent per mu, and accelerating the decomposition of the straws by using water accumulated in the furrows;|[0072] (3) mixing 5 parts of farmyard manure, 3 parts of biochar and 1.5 parts of plant ash uniformly according to a proportion from 3 late months to 4 early months of the next year, and carrying out stack retting fermentation for 18 days to completely decompose the farmyard manure;|[0073] (4) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (3) with equal quality into furrows before sowing (5 last ten days), turning over, and then planting Chinese silvergrass in the furrows;|[0074] (5) in ten days from the next month of 9 months to the last month of 10 months, after the miscanthus is harvested, turning the soil on the ridge into furrows to form new ridges, changing the original ridge back position into the furrows, then crushing the harvested miscanthus straws, wherein the length of the straws is not more than 10cm, scattering the straws into the new furrows, applying 8 kg of urea and 3 kg of straw decomposition agent per mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0075] (6) mixing 5 parts of farmyard manure, 3 parts of biological carbon and 1.5 parts of plant ash uniformly according to a proportion from 3 late ten days to 4 early ten days in spring of the third year, and composting and fermenting for 18 days to completely decompose the fertilizer;|[0076] (7) uniformly spreading the decomposed fertilizer and the compound fertilizer in the step (6) with equal quality into furrows before sowing (4 late ten days to 5 early ten days in month), ploughing, and then planting corns in the furrows;|[0077] (8) in ten days from the next month of 9 months to the last month of 10 months, after the corn is harvested, turning soil on the ridges into furrows to form new ridges, changing the positions of the backs of the original ridges into furrows, then crushing and scattering corn straws into the new furrows, applying 8 kilograms of urea and 3 kilograms of straw decomposition agents to each mu, accelerating the decay of the straws by utilizing the water accumulated in the furrows,|[0078] (9) and (5) repeating the steps (6) to (8) in the fourth year.|[0079] In the embodiment, in the step (1), the ridge height of the ridge back is 13cm, the bottom width of the ridge back is 55cm, and the ridge distance is 35 cm.|[0080] In this embodiment, the straw-decomposing inoculant in the steps (2), (5) and (8) is a four-strong straw-decomposing inoculant. It is produced by Zhongbang biotechnology, Inc. in Hebei.|[0081] In this embodiment, the farm manure in step (3) is pig manure, the biochar in step (3) is produced by using straws, and the plant ash in step (3) is ash material remaining after the combustion of firewood.|[0082] In this example, the total fertilizing amount in the step (4) is 35 kg/mu.|[0083] In the embodiment, the compound fertilizer in the step (4) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0084] In this example, the total fertilizing amount in the step (7) is 45 kg/mu.|[0085] In the embodiment, the compound fertilizer in the step (7) is a nitrogen-phosphorus-potassium compound fertilizer, the compound fertilizer contains 23% of nitrogen, the compound fertilizer contains 12% of phosphorus pentoxide, and the compound fertilizer contains 5% of potassium oxide.|[0086] The embodiments of the present invention have been described in detail. However, the present invention is not limited to the above-described embodiments, and various changes can be made within the knowledge of those skilled in the art without departing from the spirit of the present invention. Family Number|(69443585)|69443585|Abstract|(CN104641756 A)|The invention relates to a method for increasing the carbon sequestration capacity of soil of a mining area . The method comprises the steps : ( 1 ) ridging the soil ; ( 2 ) during ridging , burying crushed straws into ridge furrows and applying urea and a straw decomposition agent ; ( 3 ) composting from the last third of March to the first third of April in a next year ; ( 4 ) before sowing , fertilizing and then planting green manure crops ; ( 5 ) from the last third of September to the first third of October , ridging , spraying crushed crop straws into new ridge furrows , and applying urea and the straw decomposition agent ; ( 6 ) composting decomposed manure from the last third of March to the first third of April in a third year ; ( 7 ) before sowing , fertilizing and then planting maize ; ( 8 ) from the last third of September to the first third of October , ridging , crushing maize straws , spraying the crushed maize straws into ridge furrows , and applying urea and the straw decomposition agent ; ( 9 ) repeating the steps ( 6 ) to ( 8 ) in a fourth year . The method has the following beneficial effects that the carbon sequestration capacity of the soil of the mining area can be rapidly increased ; solid wastes of the mining area can be effectively utilized ; the consumption of chemical fertilizers is lowered , and the fertility of the soil is improved while the carbon sequestration capacity of the soil is increased ; the economic cost is low , and the operability is strong . |IPC codes|(CN104641756 A)|A01B - 079/02 |Title|(CN104641756 A)|Method for increasing carbon sequestration capacity of soil of mining area | Other special machines A01B-079/02 A01B-079/02 CN109328528B|CN107473853|CN107509406|CN114982414|CN116806477|CN114394867|CN114287194|CN112931069|CN110476534|CN109744118|CN106311735 CN109328528B 83391096 WHO=Examiner SELF=N CAT=Y|CN107473853 78099692 WHO=Examiner SELF=N CAT=Y|CN107509406 78181621 WHO=Examiner SELF=Y CAT=Y|CN114982414 101616186 WHO=Examiner SELF=N CAT=X|CN116806477 106681485 WHO=Examiner SELF=N CAT=A|CN114394867 99776540 WHO=Examiner SELF=N CAT=A|CN114287194 99507645 WHO=Examiner SELF=N CAT=A|CN112931069 94647151 WHO=Examiner SELF=N CAT=A|CN110476534 86727517 WHO=Examiner SELF=N CAT=A|CN109744118 84469820 WHO=Examiner SELF=N CAT=A|CN106311735 75129378 WHO=Examiner SELF=N CAT=A CN103125250|CN102336614|CN1596572|CN103947326|CN103392437|RU2011117840|JP2006143791 CN103125250 45358595 WHO=Examiner SELF=N CAT=Y|CN102336614 7573132 WHO=Examiner SELF=N CAT=Y|CN1596572 61969674 WHO=Examiner SELF=N CAT=Y|CN103947326 67115534 WHO=Examiner SELF=N CAT=A|CN103392437 59349830 WHO=Examiner SELF=N CAT=A|RU2011117840 36409411 WHO=Examiner SELF=N CAT=A|JP2006143791 22878832 WHO=Examiner SELF=N CAT=A 原芩等: &quot;不同管理措施对铝矿废弃地复垦区土壤有机碳的影响&quot;, 《农业环境科学学报》 (Cat. Y) CN103947326; CN103125250; CN102336614; RU2011117840; JP2006143791; CN103392437; CN1596572 REVOKED (CN104641756)|REVOKED DEAD (CN104641756)|DEAD (CN104641756)|LEGAL DETAILS FOR CN104641756|Actual or expected expiration date=2017-09-26|Legal state=DEAD|Status=REVOKED|Event publication date=2015-02-12|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201510076568|Application date=2015-02-12|Standardized application number=2015CN-0076568|Event publication date=2015-05-27|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN104641756|Publication stage code=A|Publication date=2015-05-27|Standardized publication number=CN104641756|Event publication date=2015-05-27|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2015-06-24|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2017-09-26|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjmdEznconw3EVfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=HRc2PvhtNaOF65fqGD2mXpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN104641756)|CN (CN104641756)|NAME=INSTITUTE OF AGRICULTURAL ENVIRONMENT AND RESOURCE, SHANXI ACADEMY OF AGRICULTURAL SCIENCES , COUNTRY=CN (CN104641756)|NAME=GUO GUANHOU;BEIJING SUTHINK PATENT AGENCY FIRM (ORDINARY PARTNERSHIP) (CN104641756)|NAME=ZHANG QIANG|NAME=JIN DONGSHENG|NAME=GAO CHUNHUA|NAME=LI JIANHUA|NAME=LU CHAODONG|NAME=DONG YUNZHONG|NAME=LU JINJING 0 1 Titre: (CN104641756)|Method for increasing carbon sequestration capacity of soil of mining area Résumé: (CN104641756)|The invention relates to a method for increasing the carbon sequestration capacity of soil of a mining area. The method comprises the steps: (1) ridging the soil; (2) during ridging, burying crushed straws into ridge furrows and applying urea and a straw decomposition agent; (3) composting from the last third of March to the first third of April in a next year; (4) before sowing, fertilizing and then planting green manure crops; (5) from the last third of September to the first third of October, ridging, spraying crushed crop straws into new ridge furrows, and applying urea and the straw decomposition agent; (6) composting decomposed manure from the last third of March to the first third of April in a third year; (7) before sowing, fertilizing and then planting maize; (8) from the last third of September to the first third of October, ridging, crushing maize straws, spraying the crushed maize straws into ridge furrows, and applying urea and the straw decomposition agent; (9) repeating the steps (6) to (8) in a fourth year. The method has the following beneficial effects that the carbon sequestration capacity of the soil of the mining area can be rapidly increased; solid wastes of the mining area can be effectively utilized; the consumption of chemical fertilizers is lowered, and the fertility of the soil is improved while the carbon sequestration capacity of the soil is increased; the economic cost is low, and the operability is strong. 17 Abstract gpt-4o-mini no The method focuses on soil management and composting without explicitly addressing mineral weathering or CO₂ capture through mineral carbonation.
17 CN202311676996 CN202311676996 CN117717989 108940024 CN117717989 A 2024-03-19 [CN117717989] 2023-12-07 2023-12-07 2024-03-19 (CN117717989)|2043-12-07 (CN117717989)|Lateral aeration vortex type carbon sequestration and alkali reduction rapid reaction device (CN117717989)|The invention provides a side aeration vortex type carbon sequestration and alkali reduction rapid reaction device which comprises a reaction tank, a stirring shell, a conveying pipe and an aeration pipe, the lower portion of the reaction tank is connected with the stirring shell, an impeller is arranged in the stirring shell, and the conveying pipe is connected with the stirring shell and connected with a backflow pipe and a discharging pipe through a switching valve. The aeration pipe is fixed on the side wall of the reaction tank, is positioned above the conical bottom shell and is connected with an exhaust port of the boiler through a gas conveying pipe. By arranging the stirring shell and the impeller, under the high-speed rotation effect of the impeller, slurry has a shearing and crushing effect on high-alkali solid waste, the specific surface area of a reaction molecular group is increased, alkaline substances in the high-alkali solid waste are rapidly separated out and fully dissolved in water, the phenomenon of ash in water is eliminated, solid-liquid mixing is more sufficient, and the reaction efficiency is improved; the aeration pipe can be prevented from being blocked, and the slurry can circularly flow in the reaction tank, so that the generation of precipitates is prevented. CCTEG COAL MINING RESEARCH INSTITUTE|NATIONAL ENERGY GROUP GUOYUAN POWER|TIANDI SCIENCE & TECHNOLOGY|ZHEJIANG HANGZHOU DRILLING MACHINE MANUFACTORY (CN117717989)|ZHEJIANG HANGZHOU DRILLING MACHINE MANUFACTORY CO. LTD. ([CN])|CCTEG COAL MINING RESEARCH INSTITUTE|TIANDI SCIENCE & TECHNOLOGY CO. LTD.|NATIONAL ENERGY GROUP GUOYUAN POWER CO., LTD. ZHU HUAJUN|YIN XIWEN|GAO LINJUN|LI YONGEN|DING XUHAI|GAN ZHICHAO|CHEN LI|YU QIUGE|DUAN ZHONGWEI|LIU GUI|XU GUODONG (CN117717989)|ZHU HUAJUN|YIN XIWEN|GAO LINJUN|LI YONGEN|DING XUHAI|GAN ZHICHAO|CHEN LI|YU QIUGE|DUAN ZHONGWEI|LIU GUI|XU GUODONG (CN117717989)|TIAN NING;TSINGYIHUA INTELLECTUAL PROPERTY LLC|Reg. Nb: 11201 (CN117717989)|This application is through setting up the toper drain pan, guarantees on the one hand that thick liquid does not have to remain or as little as possible remains in the retort, and on the other hand also makes the thick liquid more form the swirl in stirring in-process.| (CN117717989)|1. The utility model provides a side aeration vortex formula solid carbon falls alkali quick reaction unit which characterized in that includes: the lower part of the reaction tank is a conical bottom shell, and the bottom of the conical bottom shell is provided with a discharge hole; the stirring shell is connected with the conical bottom shell through the discharge hole, an impeller is arranged in the stirring shell, and the impeller is connected with a driving device through a rotating shaft; the conveying pipe is provided with a first port and a second port, the first port is connected with one side of the stirring shell, the second port is connected with a return pipe and a discharge pipe through a switching valve, and the outlet end of the return pipe extends into the reaction tank; the aeration pipe is provided with a plurality of aeration holes which are uniformly distributed, the aeration pipe is fixed on the side wall of the reaction tank and is positioned above the conical bottom shell, and the aeration pipe is connected with an exhaust port of the boiler through a gas pipe.| (CN117717989)|The invention aims to provide a side aeration vortex type carbon-fixing alkali-reducing rapid reaction device, which enables flue gas to be fully contacted with high-alkali solid waste slurry, and improves reaction efficiency. An embodiment of an aspect of the present application provides a side aeration vortex type carbon fixation alkali reduction quick reaction device, including: the lower part of the reaction tank is a conical bottom shell, and the bottom of the conical bottom shell is provided with a discharge hole; the stirring shell is connected with the conical bottom shell through a discharge hole, an impeller is arranged in the stirring shell, and the impeller is connected with the driving device through a rotating shaft; the conveying pipe is provided with a first port and a second port, the first port is connected with one side of the stirring shell, the second port is connected with the return pipe and the discharge pipe through a switching valve, so that materials can be controlled to enter the return pipe or the discharge pipe through switching of the switching valve, and the outlet end of the return pipe extends into the reaction tank; the aeration pipe is provided with a plurality of aeration holes which are uniformly distributed and arranged, is fixed on the side wall of the reaction tank and is positioned above the conical bottom shell, and is connected with an exhaust port of the boiler through the gas pipe.|The invention provides a side aeration vortex type carbon fixation alkali reduction rapid reaction device which comprises a reaction tank, a stirring shell, a conveying pipe and an aeration pipe, wherein the lower part of the reaction tank is connected with the stirring shell, an impeller is arranged in the stirring shell, the conveying pipe is connected with the stirring shell and is connected with a return pipe and a discharge pipe through a switching valve, the aeration pipe is fixed on the side wall of the reaction tank and is positioned above a conical bottom shell, and the aeration pipe is connected with an exhaust port of a boiler through the gas conveying pipe.|The invention relates to the technical field of high-alkali solid waste treatment, in particular to a side aeration vortex type carbon-fixing alkali-reducing rapid reaction device.| (CN117717989)|AERATION PIPE(100,22)|AERATION VORTEX(100,10)|CARBON FIXATION(100,8)|SIDE AERATION VORTEX(100,5)|ALKALI REDUCTION RAPID REACTION(100,3)|REDUCTION RAPID REACTION(100,3)|AERATION VORTEX SOLID CARBON(100,1)|ALKALI QUICK REACTION(100,1)|SOLID CARBON(100,1)|STIRRING SHELL(99,12)|AERATION VORTEX CARBON FIXING(61,8)|CONICAL BOTTOM SHELL(54,8)|REACTION TANK(53,69)|CONVEYING PIPE(50,11)|AERATION HOLE(43,5)|ROTOR(39,24)|DISCHARGE HOLE(37,6)|SWITCHING VALVE(32,14)|DISCHARGE PIPE(32,4)|RETORT(25,2)|RAPID REACTION(22,13)|ALKALI REDUCTION QUICK REACTION(22,1)|AIR INLET NOZZLE(21,10)|REDUCTION REACTION RAPIDITY(21,1)|ONLINE MONITORING PORT(20,3)|PRECIPITATION PRODUCTION(20,1)|SWIRL(19,1)|TOPER(19,1)|RETURN PIPE(18,19)|EXHAUST PORT(18,12)|GUARANTEE(18,1)|ALKALI REDUCING RAPID REACTION(17,11)|CARBON FIXING(17,8)|ALKALINE SUBSTANCE(17,3)|WATER DRUM ASH PHENOMENON(17,1)|THICK LIQUID(16,3)|REACTIVE MOLECULE GROUP(16,1)|CONICAL BOTTOM(15,7)|ALKALI SOLID WASTE(15,3)|STIRRING SHELL SIDE(15,2)|ADJACENT AERATION PIPE(15,1)|AIR DELIVERY PIPE(14,1)|CHARGING PORT(13,3)|SOLID WASTE SLURRY(12,2)|PAN(12,1)|MINERALIZATION REACTION(11,8)|WATER CHARGING(11,2)|SOLID WASTE TREATMENT(11,1)|AERATION TUBE(10,10)|CRUSHING(10,4)|SOLID WASTE(9,32)|ROTATING SHAFT(9,11)|GAS PIPE(9,5)|THICK LIQUID CIRCULATION FLOW(9,1)|BOILER TAIL GAS(8,3)|INTAKE NOZZLE(7,3)|VORTEX TYPE CARBON FIXING(7,2)|COVER PLATE(6,16)|PH VALUE(6,3)|UNDERUTILIZED BOILER(6,1)|FLUE GAS(5,12)|EARTH RESOURCE(5,2)|NOUN INTERPRETATION(5,1)|SETTING UP STIRRING SHELL(5,1)|SEALING RING(4,3)|FAST PRECIPITATION(4,2)|POSITIONAL RELATIONSHIP(4,2)|UNEVEN MIXING(4,2)|WASTE DISCHARGE(4,2)|ASH ELIMINATION(4,1)|RETORT LATERAL(4,1)|SLURRY ALKALI(4,1)|SLURRY CONCENTRATION REQUIREMENT(4,1)|BOILER UTILIZATION(3,2)|FEED INLET(3,2)|GAS WASTE(3,2)|HARM(3,2)|INSUFFICIENT REACTION(3,2)|PH METER INSERTION(3,2)|SHAFT SEAT(3,2)|SHEARING(3,2)|VALUE ONLINE MONITORING PORT(3,2)|ALKALINE MATTER(3,1)|DISCHARGE REQUIREMENT(3,1)|EXPOSURETHE AIR PIPE PREVENTION(3,1)|MATING COMPRESSION(3,1)|MINED OIL(3,1)| (CN117717989)|1. The invention provides a side aeration vortex formula solid carbon falls alkali quick reaction unit which characterized in that includes:|the lower part of the reaction tank is a conical bottom shell, and the bottom of the conical bottom shell is provided with a discharge hole;|the stirring shell is connected with the conical bottom shell through the discharge hole, an impeller is arranged in the stirring shell, and the impeller is connected with a driving device through a rotating shaft;|the conveying pipe is provided with a first port and a second port, the first port is connected with one side of the stirring shell, the second port is connected with a return pipe and a discharge pipe through a switching valve, and the outlet end of the return pipe extends into the reaction tank;|the aeration pipe is provided with a plurality of aeration holes which are uniformly distributed, the aeration pipe is fixed on the side wall of the reaction tank and is positioned above the conical bottom shell, and the aeration pipe is connected with an exhaust port of the boiler through a gas pipe.|2. The side-part aeration vortex type carbon-fixing alkali-reducing rapid reaction device according to claim 1, wherein a plurality of aeration pipes are horizontally arranged.|3. The side-part aeration vortex type carbon-fixing alkali-reducing rapid reaction device according to claim 1, wherein the aeration pipe is annular, and the rotating shaft penetrates through the center of the aeration pipe.|4. The side-part aeration vortex type carbon-fixing alkali-reducing rapid reaction device according to claim 2, wherein the aeration holes are alternately arranged on the upper end face and the lower end face of the aeration pipe.|5. The rapid reaction device for side-part aeration vortex type carbon fixation and alkali reduction according to claim 2, wherein the aeration pipe is provided with an air inlet nozzle, the air inlet nozzle is fixed on the side wall of the reaction tank in a sealing way and extends out of the reaction tank, and the air inlet nozzle is detachably connected with the air delivery pipe.|6. The rapid reaction device for side-aeration vortex carbon fixation and alkali reduction according to claim 5, wherein the air inlet nozzles of two adjacent aeration pipes are respectively positioned on different sides of the reaction tank.|7. The side-aeration vortex carbon-fixing alkali-reducing rapid reaction device according to claim 1, wherein the first port is located on one side of the impeller and is close to the impeller.|8. The side-aeration vortex type carbon-fixing alkali-reducing rapid reaction device according to any one of claims 1 to 7, wherein a cover plate is arranged on the top of the reaction tank in an openable and closable manner.|9. The side-part aeration vortex type carbon-fixing alkali-reducing rapid reaction device according to claim 8, wherein the cover plate is provided with a charging port, a water charging port, an exhaust port and a pH value on-line monitoring port, and the driving device is arranged at the upper end of the cover plate.|10. The side-aeration vortex type carbon-fixing alkali-reducing rapid reaction device according to claim 8, wherein a sealing ring used for being matched and pressed with the reaction tank is arranged at the lower end of the cover plate. (CN117717989)|TECHNICAL FIELD|[0001] The invention relates to the technical field of high-alkali solid waste treatment, in particular to a side aeration vortex type carbon-fixing alkali-reducing rapid reaction device.|BACKGROUND ART|[0002] The high-alkali solid waste and the flue gas are main solid waste and gas waste discharged by the coal-fired power plant, and the waste discharge amount of the coal-fired power plant is increased year by year along with the development of the electric power industry. The high-alkali solid waste is characterized by high alkali metal content, and if the high-alkali solid waste is stacked on site, land resources are wasted, and the harm to the atmosphere and underground water is caused; and the direct discharge of the flue gas will cause harm to the environment.|[0003] In the prior art, high-alkali solid waste and flue gas are treated by a reaction tank generally, and the condition of uneven mixing often occurs, so that the flue gas cannot be fully contacted with slurry of the high-alkali solid waste, and then insufficient reaction is caused, the mineralization reaction is affected, and the waste treatment efficiency is further affected. Moreover, the existing stirring device adopts a propeller structure, so that slurry is easy to precipitate, and an aeration pipe is usually arranged at the bottom of the reaction tank and is easy to be blocked if precipitation occurs.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a side aeration vortex type carbon-fixing alkali-reducing rapid reaction device, which enables flue gas to be fully contacted with high-alkali solid waste slurry, and improves reaction efficiency.|[0005] An embodiment of an aspect of the present application provides a side aeration vortex type carbon fixation alkali reduction quick reaction device, including: the lower part of the reaction tank is a conical bottom shell, and the bottom of the conical bottom shell is provided with a discharge hole; the stirring shell is connected with the conical bottom shell through a discharge hole, an impeller is arranged in the stirring shell, and the impeller is connected with the driving device through a rotating shaft; the conveying pipe is provided with a first port and a second port, the first port is connected with one side of the stirring shell, the second port is connected with the return pipe and the discharge pipe through a switching valve, so that materials can be controlled to enter the return pipe or the discharge pipe through switching of the switching valve, and the outlet end of the return pipe extends into the reaction tank; the aeration pipe is provided with a plurality of aeration holes which are uniformly distributed and arranged, is fixed on the side wall of the reaction tank and is positioned above the conical bottom shell, and is connected with an exhaust port of the boiler through the gas pipe.|[0006] According to the high-alkali solid waste alkaline material (OH), the stirring shell and the impeller are arranged, the slurry has a shearing and crushing effect on the high-alkali solid waste under the high-speed rotation effect of the impeller, the specific surface area of the reactive molecular group is increased, and the alkaline material (OH) in the high-alkali solid waste is formed - ) Fast precipitation, full dissolution in water, elimination of ash in water, more full solid-liquid mixing, high reaction efficiency and prevention of exposureThe air pipe is blocked, and the slurry can circulate in the reaction tank to prevent the generation of sediment.|[0007] The side wall of the reaction tank is provided with the aeration pipe, so that the aeration pipe can be prevented from being blocked.|[0008] According to the device, the switching valve is arranged on the conveying pipe, the slurry is controlled to enter the return pipe or the discharge pipe through switching of the switching valve, so that the slurry reacted in the reaction tank can be selectively reentered the reaction tank from the return pipe, or is discharged to the next equipment from the discharge pipe, and the reaction process is controlled.|[0009] This application is through setting up the toper drain pan, guarantees on the one hand that thick liquid does not have to remain or as little as possible remains in the retort, and on the other hand also makes the thick liquid more form the swirl in stirring in-process.|[0010] In some embodiments, the aeration tube is provided in a plurality and horizontally disposed.|[0011] This application is through setting up a plurality of aeration pipes at the retort lateral part, under the effect of the vortex that the impeller formed, bubble dispersion is more even for boiler tail gas fully contacts with the thick liquid of high alkali solid waste, and the reaction is more abundant, has improved mass transfer efficiency and reaction efficiency.|[0012] In some embodiments, the aeration tube is annular, and the rotating shaft penetrates through the center of the aeration tube.|[0013] In some embodiments, the aeration holes are staggered in the upper and lower end surfaces of the aeration tube. The flue gas is thoroughly mixed with the slurry.|[0014] In some embodiments, the aeration pipe is provided with an air inlet nozzle, the air inlet nozzle is fixed on the side wall of the reaction tank in a sealing way and extends out of the reaction tank, and the air inlet nozzle is detachably connected with the air pipe. The plurality of aeration pipes are connected with the gas pipe in parallel through the gas inlet pipe nozzles, and can simultaneously convey the tail gas of the boiler in the reaction tank, so that the reaction is more sufficient.|[0015] In some embodiments, the intake nozzles of adjacent two aeration tubes are located on different sides of the reaction tank, respectively.|[0016] In some embodiments, the first port is located on one side of the impeller and is proximate to the impeller. The slurry can be directly conveyed into the conveying pipe through the rotation of the impeller, so that the slurry can flow circularly in the reaction tank.|[0017] In some embodiments, a cover plate is arranged on the top of the reaction tank in an openable and closable manner. The internal structure of the reaction tank can be conveniently repaired and maintained in an opening and closing mode.|[0018] In some embodiments, the cover plate is provided with a charging port, a water charging port, an air exhaust port and a pH value online monitoring port, and the driving device is arranged at the upper end of the cover plate. The feed inlet is used for adding high-alkali solid waste into the reaction tank, the water inlet is used for adding water into the reaction tank, the exhaust port is used for discharging the underutilized boiler tail gas through the exhaust port, the pH value on-line monitoring port is used for inserting a pH meter into the reaction tank so as to monitor the pH value of the slurry on line, and the slurry is controlled to enter the return pipe or the discharge pipe through the pH value of the slurry.|[0019] In some embodiments, the lower end of the cover plate is provided with a sealing ring for being matched and pressed with the reaction tank. When the cover plate is closed, the cover plate is in sealing connection with the reaction tank.|DRAWINGS DESCRIPTION|[0020] The foregoing and/or additional aspects and advantages of the present invention will become apparent and may be better understood from the following description of embodiments with reference to the accompanying drawings,|[0021] wherein:|[0022] FIG. 1 is a schematic structural diagram of a side-part aeration vortex type carbon-fixing alkali-reducing rapid reaction device;|[0023] FIG. 2 is a top view of FIG. 1;|[0024] FIG. 3 is a schematic view of the structure of the aerator pipe in FIG. 1;|[0025] reference numerals:|[0026] 1-a shaft seat; 2-rotating shaft; 3-a return pipe; 4-switching valves; 5-discharging pipe; 6-a conical bottom shell; 7-a conveying pipe; 8-exposing pores; 9-an impeller; 10-stirring the shell; 11-a motor base; 12-an electric motor; 13-cover plate; 14-a reaction tank; 15-an aeration pipe; 16-an intake nozzle; 17-supporting legs; 18-a load cell; 19-an online pH value monitoring port; 20-a charging port; 21-an exhaust port; 22-water filling port.|INVENTION MODE|Detailed Description|[0027] Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below by referring to the drawings are illustrative and intended to explain the present invention and should not be construed as limiting the invention.|[0028] Noun interpretation:|[0029] carbon sequestration refers to a measure of increasing the carbon content of a carbon reservoir other than the atmosphere. Including physical carbon fixation and biological carbon fixation. Physical carbon sequestration is the long term storage of carbon dioxide in mined oil and gas wells, coal seams, and deep seas. Biosolids are the conversion of carbon dioxide in the atmosphere, which is inorganic carbon, to organic carbon, which is carbohydrate, and are immobilized in plants or in soil. In this application, carbon sequestration refers to the reaction of carbon dioxide in flue gas by passing it into a slurry, sealing the carbon dioxide in the slurry, thereby reducing the carbon dioxide content emitted to the atmosphere.|[0030] The high-alkali solid waste and the flue gas are main solid waste and gas waste discharged by the coal-fired power plant, and the waste discharge amount of the coal-fired power plant is increased year by year along with the development of the electric power industry. The high-alkali solid waste is characterized by high alkali metal content, and if the high-alkali solid waste is stacked on site, land resources are wasted, and the harm to the atmosphere and underground water is caused; and the direct discharge of the flue gas will cause harm to the environment.|[0031] In the prior art, high-alkali solid waste and flue gas are treated by a reaction tank generally, and the condition of uneven mixing often occurs, so that the flue gas cannot be fully contacted with slurry of the high-alkali solid waste, and then insufficient reaction is caused, the mineralization reaction is affected, and the waste treatment efficiency is further affected.|[0032] The side aeration vortex type carbon fixation and alkali reduction rapid reaction device according to the embodiment of the invention is described below with reference to the accompanying drawings.|[0033] As shown in fig. 1-3, an embodiment of the present application provides a side aeration vortex type carbon-fixing alkali-reducing rapid reaction device, including: the device comprises a reaction tank 14, a stirring shell 10, a conveying pipe 7 and an aeration pipe 15, wherein the lower part of the reaction tank 14 is provided with a conical bottom shell 6, and the bottom of the conical bottom shell 6 is provided with a discharge hole; the stirring shell 10 is connected with the conical bottom shell 6 through a discharge hole, an impeller 9 is arranged in the stirring shell 10, and the impeller 9 is connected with a driving device through a rotating shaft 2; the conveying pipe 7 is provided with a first port and a second port, the first port is connected with one side of the stirring shell 10, the second port is connected with the return pipe 3 and the discharge pipe 5 through the switching valve 4, so that the material is controlled to enter the return pipe 3 or the discharge pipe 5 through the switching of the switching valve 4, and the outlet end of the return pipe 3 extends into the reaction tank 14; the aeration pipe 15 is provided with a plurality of aeration holes 8 which are uniformly distributed, the aeration pipe 15 is fixed on the side wall of the reaction tank 14 and is positioned above the conical bottom shell 6, and the aeration pipe 15 is connected with an exhaust port 21 of the boiler through a gas pipe.|[0034] According to the high-alkali solid waste alkaline material (OH), the stirring shell 10 and the impeller 9 are arranged, the slurry has a shearing and crushing effect on the high-alkali solid waste under the high-speed rotation effect of the impeller 9, the specific surface area of a reaction molecular group is increased, and alkaline substances (OH) in the high-alkali solid waste are caused - ) The slurry is quickly separated out and fully dissolved in water, so that ash in water phenomenon is eliminated, solid-liquid mixing is more complete, reaction efficiency is improved, the aeration pipe 15 is prevented from being blocked, slurry can circularly flow in the reaction tank 14, and precipitation is prevented.|[0035] The slurry is spirally moved in the reaction tank 14 and circulated by the impeller 9, so that the slurry is not precipitated and the aeration pipe 15 is not blocked.|[0036] The application can also prevent the aeration pipe 15 from blocking by arranging the aeration pipe 15 on the side wall of the reaction tank 14. By side aeration, the gas is rotated together with the slurry in the reaction tank 14, the movement path is prolonged, the time of contact with the slurry is prolonged, and the reaction efficiency is improved.|[0037] The transfer pipe 7 is provided with the switching valve 4, and the slurry is controlled to enter the return pipe 3 or the discharge pipe 5 through the switching of the switching valve 4, so that the slurry reacted in the reaction tank 14 can be selectively reentered into the reaction tank 14 from the return pipe 3 or discharged to the next equipment from the discharge pipe 5, thereby controlling the reaction process.|[0038] The conical bottom shell 6 is arranged, so that slurry is ensured to be free from residues or less residues as much as possible in the reaction tank 14, and the slurry is easier to form vortex in the stirring process.|[0039] Further, water is added into the reaction tank 14, the impeller 9 is started to rotate, high-alkali solid waste is added into the reaction tank 14, slurry is prepared by stirring of the impeller 9, and then boiler tail gas is introduced into the reaction tank 14 through the aeration pipe 15 to be mixed with the slurry for mineralization reaction. The slurry after mineralization reaction enters a conveying pipe 7, and the slurry after mineralization reaction can be selectively reentered into a reaction tank 14 from a return pipe 3 or discharged from a discharge pipe 5 by controlling a switching valve 4.|[0040] In some embodiments, the aeration tube 15 is provided in a plurality and horizontally disposed.|[0041] According to the method, the plurality of aeration pipes 15 are arranged on the side part of the reaction tank 14, bubbles are dispersed more uniformly under the action of vortex formed by the impeller 9, so that the boiler tail gas is fully contacted with the high-alkali solid waste slurry, the reaction is more complete, and the mass transfer efficiency and the reaction efficiency are improved.|[0042] In some embodiments, the aeration tube 15 is ring-shaped, and the rotating shaft 2 penetrates through the center of the aeration tube 15.|[0043] In some embodiments, aeration holes 8 are staggered on the upper and lower end surfaces of aeration tube 15. The flue gas is thoroughly mixed with the slurry.|[0044] In some embodiments, the aeration pipe 15 has an air inlet nozzle 16, the air inlet nozzle 16 is fixed on the side wall of the reaction tank 14 in a sealing way and extends out of the reaction tank 14, and the air inlet nozzle 16 is detachably connected with the air pipe. The plurality of aeration pipes 15 are connected in parallel with one gas pipe through the gas inlet pipe nozzles 16, and can simultaneously convey the tail gas of the boiler in the reaction tank 14, so that the reaction is more sufficient.|[0045] In some embodiments, the intake nozzles 16 of adjacent two aeration tubes 15 are located on different sides of the reaction tank 14, respectively.|[0046] In some embodiments, the first port is located on one side of the impeller 9 and is proximate to the impeller 9. The slurry can be directly conveyed into the conveying pipe 7 by the rotation of the impeller 9, and the slurry can flow circularly in the reaction tank 14 more conveniently.|[0047] In some embodiments, a cover plate 13 is provided on the top of the reaction tank 14 in an openable and closable manner. The inner structure of the reaction tank 14 can be easily repaired and maintained by opening and closing.|[0048] In some embodiments, the cover 13 has a feed inlet 20, a water inlet 22, an exhaust outlet 21, and an online pH monitoring port 19, and the driving device is disposed at the upper end of the cover 13. The feed port 20 is used for adding high-alkali solid waste into the reaction tank 14, the water inlet 22 is used for adding water into the reaction tank 14, the exhaust port 21 is used for discharging underutilized boiler tail gas through the exhaust port 21, the pH value online monitoring port 19 is used for inserting a pH meter into the reaction tank 14 so as to online monitor the pH value of slurry, and the slurry is controlled to enter the return pipe 3 or the discharge pipe 5 through the pH value of the slurry. When the pH is not reached, the slurry re-enters the reaction tank 14 from the return pipe 3. When the pH value reaches the requirement, the flow direction of the slurry is switched by the switching valve 4, so that the slurry is discharged to the next equipment through the discharge pipe 5.|[0049] Further, the exhaust port 21 may be connected to an exhaust gas purifying device to prevent atmospheric pollution.|[0050] Further, the driving device comprises a motor 12, a motor 12 seat 11 and a shaft seat 1, the rotating shaft 2 is arranged on the shaft seat 1, the motor 12 is arranged on the cover plate 13 through the motor 12 seat 11, the motor 12 is connected with the rotating shaft 2 through a transmission mechanism such as a gear and a chain and drives the rotating shaft 2 to rotate, and then the impeller 9 is driven to rotate.|[0051] Further, the feeding port 20 and the pH value on-line monitoring port 19 are respectively positioned at two sides of the driving device.|[0052] In some embodiments, the lower end of the cover plate 13 has a sealing ring for mating compression with the reaction tank 14. When the cover plate 13 is closed, the cover plate 13 is in sealing connection with the reaction tank 14.|[0053] In some embodiments, the reaction tank 14 is provided with a load cell 18 for controlling the quality of the added high alkali solid waste and water to meet the slurry concentration requirements. Load cell 18 may be mounted on leg 17 of canister 14. The manner and type of installation of the load cell 18 is known in the art and will not be described in detail herein.|[0054] When in use, the method comprises the following steps:|[0055] (1) Water is added into the reaction tank 14 through the water adding port 22, and the mass of the added water is controlled through the weighing sensor 18;|[0056] (2) The motor 12 is operated to drive the rotating shaft 2 and the impeller 9 to rotate;|[0057] (3) Adding high-alkali solid waste into the reaction tank 14 through a feed port 20, and mixing with water to form slurry, wherein the quality of the added high-alkali solid waste is controlled through a weighing sensor 18, so that the slurry meets the concentration requirement;|[0058] (4) The boiler tail gas and the boiler are introduced into the reaction tank 14 through the aeration pipe 15CO in furnace tail gas 2 Mineralizing reaction with alkaline matters in the high-alkali solid waste;|[0059] (5) Suction is generated under the high-speed rotation of the impeller 9, the tail gas of the boiler and the slurry enter the stirring shell 10 at the same time to carry out mineralization reaction, the slurry continuously flows circularly under the high-speed rotation of the impeller 9, and the slurry has shearing and crushing effects on the high-alkali solid waste, so that alkaline substances (OH - ) Fast precipitation;|[0060] (6) The slurry after mineralization reaction enters a conveying pipe 7, and the slurry after mineralization reaction reenters a reaction tank 14 through a return pipe 3 by a switching valve 4;|[0061] (7) Underutilized boiler tail gas is discharged through the exhaust port 21;|[0062] (8) After the alkali of the slurry in the reaction tank 14 is reduced to meet the discharge requirement, namely, after the pH value reaches the requirement, the flow direction of the slurry is switched by the switching valve 4, so that the slurry is discharged through the discharge pipe 5.|[0063] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.|[0064] Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.|[0065] In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; may be mechanically connected, may be electrically connected or may be in communication with each other; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.|[0066] In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.|[0067] For purposes of this disclosure, the terms "one embodiment," "some embodiments," "example," "a particular example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.|[0068] While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention. (CN117717989)|TECHNICAL FIELD|[0001] The invention relates to the technical field of high-alkali solid waste treatment, in particular to a side aeration vortex type carbon-fixing alkali-reducing rapid reaction device.|BACKGROUND ART|[0002] The high-alkali solid waste and the flue gas are main solid waste and gas waste discharged by the coal-fired power plant, and the waste discharge amount of the coal-fired power plant is increased year by year along with the development of the electric power industry. The high-alkali solid waste is characterized by high alkali metal content, and if the high-alkali solid waste is stacked on site, land resources are wasted, and the harm to the atmosphere and underground water is caused; and the direct discharge of the flue gas will cause harm to the environment.|[0003] In the prior art, high-alkali solid waste and flue gas are treated by a reaction tank generally, and the condition of uneven mixing often occurs, so that the flue gas cannot be fully contacted with slurry of the high-alkali solid waste, and then insufficient reaction is caused, the mineralization reaction is affected, and the waste treatment efficiency is further affected. Moreover, the existing stirring device adopts a propeller structure, so that slurry is easy to precipitate, and an aeration pipe is usually arranged at the bottom of the reaction tank and is easy to be blocked if precipitation occurs.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a side aeration vortex type carbon-fixing alkali-reducing rapid reaction device, which enables flue gas to be fully contacted with high-alkali solid waste slurry, and improves reaction efficiency.|[0005] An embodiment of an aspect of the present application provides a side aeration vortex type carbon fixation alkali reduction quick reaction device, including: the lower part of the reaction tank is a conical bottom shell, and the bottom of the conical bottom shell is provided with a discharge hole; the stirring shell is connected with the conical bottom shell through a discharge hole, an impeller is arranged in the stirring shell, and the impeller is connected with the driving device through a rotating shaft; the conveying pipe is provided with a first port and a second port, the first port is connected with one side of the stirring shell, the second port is connected with the return pipe and the discharge pipe through a switching valve, so that materials can be controlled to enter the return pipe or the discharge pipe through switching of the switching valve, and the outlet end of the return pipe extends into the reaction tank; the aeration pipe is provided with a plurality of aeration holes which are uniformly distributed and arranged, is fixed on the side wall of the reaction tank and is positioned above the conical bottom shell, and is connected with an exhaust port of the boiler through the gas pipe.|[0006] According to the high-alkali solid waste alkaline material (OH), the stirring shell and the impeller are arranged, the slurry has a shearing and crushing effect on the high-alkali solid waste under the high-speed rotation effect of the impeller, the specific surface area of the reactive molecular group is increased, and the alkaline material (OH) in the high-alkali solid waste is formed - ) Fast precipitation, full dissolution in water, elimination of ash in water, more full solid-liquid mixing, high reaction efficiency and prevention of exposureThe air pipe is blocked, and the slurry can circulate in the reaction tank to prevent the generation of sediment.|[0007] The side wall of the reaction tank is provided with the aeration pipe, so that the aeration pipe can be prevented from being blocked.|[0008] According to the device, the switching valve is arranged on the conveying pipe, the slurry is controlled to enter the return pipe or the discharge pipe through switching of the switching valve, so that the slurry reacted in the reaction tank can be selectively reentered the reaction tank from the return pipe, or is discharged to the next equipment from the discharge pipe, and the reaction process is controlled.|[0009] This application is through setting up the toper drain pan, guarantees on the one hand that thick liquid does not have to remain or as little as possible remains in the retort, and on the other hand also makes the thick liquid more form the swirl in stirring in-process.|[0010] In some embodiments, the aeration tube is provided in a plurality and horizontally disposed.|[0011] This application is through setting up a plurality of aeration pipes at the retort lateral part, under the effect of the vortex that the impeller formed, bubble dispersion is more even for boiler tail gas fully contacts with the thick liquid of high alkali solid waste, and the reaction is more abundant, has improved mass transfer efficiency and reaction efficiency.|[0012] In some embodiments, the aeration tube is annular, and the rotating shaft penetrates through the center of the aeration tube.|[0013] In some embodiments, the aeration holes are staggered in the upper and lower end surfaces of the aeration tube. The flue gas is thoroughly mixed with the slurry.|[0014] In some embodiments, the aeration pipe is provided with an air inlet nozzle, the air inlet nozzle is fixed on the side wall of the reaction tank in a sealing way and extends out of the reaction tank, and the air inlet nozzle is detachably connected with the air pipe. The plurality of aeration pipes are connected with the gas pipe in parallel through the gas inlet pipe nozzles, and can simultaneously convey the tail gas of the boiler in the reaction tank, so that the reaction is more sufficient.|[0015] In some embodiments, the intake nozzles of adjacent two aeration tubes are located on different sides of the reaction tank, respectively.|[0016] In some embodiments, the first port is located on one side of the impeller and is proximate to the impeller. The slurry can be directly conveyed into the conveying pipe through the rotation of the impeller, so that the slurry can flow circularly in the reaction tank.|[0017] In some embodiments, a cover plate is arranged on the top of the reaction tank in an openable and closable manner. The internal structure of the reaction tank can be conveniently repaired and maintained in an opening and closing mode.|[0018] In some embodiments, the cover plate is provided with a charging port, a water charging port, an air exhaust port and a pH value online monitoring port, and the driving device is arranged at the upper end of the cover plate. The feed inlet is used for adding high-alkali solid waste into the reaction tank, the water inlet is used for adding water into the reaction tank, the exhaust port is used for discharging the underutilized boiler tail gas through the exhaust port, the pH value on-line monitoring port is used for inserting a pH meter into the reaction tank so as to monitor the pH value of the slurry on line, and the slurry is controlled to enter the return pipe or the discharge pipe through the pH value of the slurry.|[0019] In some embodiments, the lower end of the cover plate is provided with a sealing ring for being matched and pressed with the reaction tank. When the cover plate is closed, the cover plate is in sealing connection with the reaction tank.|DRAWINGS DESCRIPTION|[0020] The foregoing and/or additional aspects and advantages of the present invention will become apparent and may be better understood from the following description of embodiments with reference to the accompanying drawings,|[0021] wherein:|[0022] FIG. 1 is a schematic structural diagram of a side-part aeration vortex type carbon-fixing alkali-reducing rapid reaction device;|[0023] FIG. 2 is a top view of FIG. 1;|[0024] FIG. 3 is a schematic view of the structure of the aerator pipe in FIG. 1;|[0025] reference numerals:|[0026] 1-a shaft seat; 2-rotating shaft; 3-a return pipe; 4-switching valves; 5-discharging pipe; 6-a conical bottom shell; 7-a conveying pipe; 8-exposing pores; 9-an impeller; 10-stirring the shell; 11-a motor base; 12-an electric motor; 13-cover plate; 14-a reaction tank; 15-an aeration pipe; 16-an intake nozzle; 17-supporting legs; 18-a load cell; 19-an online pH value monitoring port; 20-a charging port; 21-an exhaust port; 22-water filling port.|INVENTION MODE|Detailed Description|[0027] Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below by referring to the drawings are illustrative and intended to explain the present invention and should not be construed as limiting the invention.|[0028] Noun interpretation:|[0029] carbon sequestration refers to a measure of increasing the carbon content of a carbon reservoir other than the atmosphere. Including physical carbon fixation and biological carbon fixation. Physical carbon sequestration is the long term storage of carbon dioxide in mined oil and gas wells, coal seams, and deep seas. Biosolids are the conversion of carbon dioxide in the atmosphere, which is inorganic carbon, to organic carbon, which is carbohydrate, and are immobilized in plants or in soil. In this application, carbon sequestration refers to the reaction of carbon dioxide in flue gas by passing it into a slurry, sealing the carbon dioxide in the slurry, thereby reducing the carbon dioxide content emitted to the atmosphere.|[0030] The high-alkali solid waste and the flue gas are main solid waste and gas waste discharged by the coal-fired power plant, and the waste discharge amount of the coal-fired power plant is increased year by year along with the development of the electric power industry. The high-alkali solid waste is characterized by high alkali metal content, and if the high-alkali solid waste is stacked on site, land resources are wasted, and the harm to the atmosphere and underground water is caused; and the direct discharge of the flue gas will cause harm to the environment.|[0031] In the prior art, high-alkali solid waste and flue gas are treated by a reaction tank generally, and the condition of uneven mixing often occurs, so that the flue gas cannot be fully contacted with slurry of the high-alkali solid waste, and then insufficient reaction is caused, the mineralization reaction is affected, and the waste treatment efficiency is further affected.|[0032] The side aeration vortex type carbon fixation and alkali reduction rapid reaction device according to the embodiment of the invention is described below with reference to the accompanying drawings.|[0033] As shown in fig. 1-3, an embodiment of the present application provides a side aeration vortex type carbon-fixing alkali-reducing rapid reaction device, including: the device comprises a reaction tank 14, a stirring shell 10, a conveying pipe 7 and an aeration pipe 15, wherein the lower part of the reaction tank 14 is provided with a conical bottom shell 6, and the bottom of the conical bottom shell 6 is provided with a discharge hole; the stirring shell 10 is connected with the conical bottom shell 6 through a discharge hole, an impeller 9 is arranged in the stirring shell 10, and the impeller 9 is connected with a driving device through a rotating shaft 2; the conveying pipe 7 is provided with a first port and a second port, the first port is connected with one side of the stirring shell 10, the second port is connected with the return pipe 3 and the discharge pipe 5 through the switching valve 4, so that the material is controlled to enter the return pipe 3 or the discharge pipe 5 through the switching of the switching valve 4, and the outlet end of the return pipe 3 extends into the reaction tank 14; the aeration pipe 15 is provided with a plurality of aeration holes 8 which are uniformly distributed, the aeration pipe 15 is fixed on the side wall of the reaction tank 14 and is positioned above the conical bottom shell 6, and the aeration pipe 15 is connected with an exhaust port 21 of the boiler through a gas pipe.|[0034] According to the high-alkali solid waste alkaline material (OH), the stirring shell 10 and the impeller 9 are arranged, the slurry has a shearing and crushing effect on the high-alkali solid waste under the high-speed rotation effect of the impeller 9, the specific surface area of a reaction molecular group is increased, and alkaline substances (OH) in the high-alkali solid waste are caused - ) The slurry is quickly separated out and fully dissolved in water, so that ash in water phenomenon is eliminated, solid-liquid mixing is more complete, reaction efficiency is improved, the aeration pipe 15 is prevented from being blocked, slurry can circularly flow in the reaction tank 14, and precipitation is prevented.|[0035] The slurry is spirally moved in the reaction tank 14 and circulated by the impeller 9, so that the slurry is not precipitated and the aeration pipe 15 is not blocked.|[0036] The application can also prevent the aeration pipe 15 from blocking by arranging the aeration pipe 15 on the side wall of the reaction tank 14. By side aeration, the gas is rotated together with the slurry in the reaction tank 14, the movement path is prolonged, the time of contact with the slurry is prolonged, and the reaction efficiency is improved.|[0037] The transfer pipe 7 is provided with the switching valve 4, and the slurry is controlled to enter the return pipe 3 or the discharge pipe 5 through the switching of the switching valve 4, so that the slurry reacted in the reaction tank 14 can be selectively reentered into the reaction tank 14 from the return pipe 3 or discharged to the next equipment from the discharge pipe 5, thereby controlling the reaction process.|[0038] The conical bottom shell 6 is arranged, so that slurry is ensured to be free from residues or less residues as much as possible in the reaction tank 14, and the slurry is easier to form vortex in the stirring process.|[0039] Further, water is added into the reaction tank 14, the impeller 9 is started to rotate, high-alkali solid waste is added into the reaction tank 14, slurry is prepared by stirring of the impeller 9, and then boiler tail gas is introduced into the reaction tank 14 through the aeration pipe 15 to be mixed with the slurry for mineralization reaction. The slurry after mineralization reaction enters a conveying pipe 7, and the slurry after mineralization reaction can be selectively reentered into a reaction tank 14 from a return pipe 3 or discharged from a discharge pipe 5 by controlling a switching valve 4.|[0040] In some embodiments, the aeration tube 15 is provided in a plurality and horizontally disposed.|[0041] According to the method, the plurality of aeration pipes 15 are arranged on the side part of the reaction tank 14, bubbles are dispersed more uniformly under the action of vortex formed by the impeller 9, so that the boiler tail gas is fully contacted with the high-alkali solid waste slurry, the reaction is more complete, and the mass transfer efficiency and the reaction efficiency are improved.|[0042] In some embodiments, the aeration tube 15 is ring-shaped, and the rotating shaft 2 penetrates through the center of the aeration tube 15.|[0043] In some embodiments, aeration holes 8 are staggered on the upper and lower end surfaces of aeration tube 15. The flue gas is thoroughly mixed with the slurry.|[0044] In some embodiments, the aeration pipe 15 has an air inlet nozzle 16, the air inlet nozzle 16 is fixed on the side wall of the reaction tank 14 in a sealing way and extends out of the reaction tank 14, and the air inlet nozzle 16 is detachably connected with the air pipe. The plurality of aeration pipes 15 are connected in parallel with one gas pipe through the gas inlet pipe nozzles 16, and can simultaneously convey the tail gas of the boiler in the reaction tank 14, so that the reaction is more sufficient.|[0045] In some embodiments, the intake nozzles 16 of adjacent two aeration tubes 15 are located on different sides of the reaction tank 14, respectively.|[0046] In some embodiments, the first port is located on one side of the impeller 9 and is proximate to the impeller 9. The slurry can be directly conveyed into the conveying pipe 7 by the rotation of the impeller 9, and the slurry can flow circularly in the reaction tank 14 more conveniently.|[0047] In some embodiments, a cover plate 13 is provided on the top of the reaction tank 14 in an openable and closable manner. The inner structure of the reaction tank 14 can be easily repaired and maintained by opening and closing.|[0048] In some embodiments, the cover 13 has a feed inlet 20, a water inlet 22, an exhaust outlet 21, and an online pH monitoring port 19, and the driving device is disposed at the upper end of the cover 13. The feed port 20 is used for adding high-alkali solid waste into the reaction tank 14, the water inlet 22 is used for adding water into the reaction tank 14, the exhaust port 21 is used for discharging underutilized boiler tail gas through the exhaust port 21, the pH value online monitoring port 19 is used for inserting a pH meter into the reaction tank 14 so as to online monitor the pH value of slurry, and the slurry is controlled to enter the return pipe 3 or the discharge pipe 5 through the pH value of the slurry. When the pH is not reached, the slurry re-enters the reaction tank 14 from the return pipe 3. When the pH value reaches the requirement, the flow direction of the slurry is switched by the switching valve 4, so that the slurry is discharged to the next equipment through the discharge pipe 5.|[0049] Further, the exhaust port 21 may be connected to an exhaust gas purifying device to prevent atmospheric pollution.|[0050] Further, the driving device comprises a motor 12, a motor 12 seat 11 and a shaft seat 1, the rotating shaft 2 is arranged on the shaft seat 1, the motor 12 is arranged on the cover plate 13 through the motor 12 seat 11, the motor 12 is connected with the rotating shaft 2 through a transmission mechanism such as a gear and a chain and drives the rotating shaft 2 to rotate, and then the impeller 9 is driven to rotate.|[0051] Further, the feeding port 20 and the pH value on-line monitoring port 19 are respectively positioned at two sides of the driving device.|[0052] In some embodiments, the lower end of the cover plate 13 has a sealing ring for mating compression with the reaction tank 14. When the cover plate 13 is closed, the cover plate 13 is in sealing connection with the reaction tank 14.|[0053] In some embodiments, the reaction tank 14 is provided with a load cell 18 for controlling the quality of the added high alkali solid waste and water to meet the slurry concentration requirements. Load cell 18 may be mounted on leg 17 of canister 14. The manner and type of installation of the load cell 18 is known in the art and will not be described in detail herein.|[0054] When in use, the method comprises the following steps:|[0055] (1) Water is added into the reaction tank 14 through the water adding port 22, and the mass of the added water is controlled through the weighing sensor 18;|[0056] (2) The motor 12 is operated to drive the rotating shaft 2 and the impeller 9 to rotate;|[0057] (3) Adding high-alkali solid waste into the reaction tank 14 through a feed port 20, and mixing with water to form slurry, wherein the quality of the added high-alkali solid waste is controlled through a weighing sensor 18, so that the slurry meets the concentration requirement;|[0058] (4) The boiler tail gas and the boiler are introduced into the reaction tank 14 through the aeration pipe 15CO in furnace tail gas 2 Mineralizing reaction with alkaline matters in the high-alkali solid waste;|[0059] (5) Suction is generated under the high-speed rotation of the impeller 9, the tail gas of the boiler and the slurry enter the stirring shell 10 at the same time to carry out mineralization reaction, the slurry continuously flows circularly under the high-speed rotation of the impeller 9, and the slurry has shearing and crushing effects on the high-alkali solid waste, so that alkaline substances (OH - ) Fast precipitation;|[0060] (6) The slurry after mineralization reaction enters a conveying pipe 7, and the slurry after mineralization reaction reenters a reaction tank 14 through a return pipe 3 by a switching valve 4;|[0061] (7) Underutilized boiler tail gas is discharged through the exhaust port 21;|[0062] (8) After the alkali of the slurry in the reaction tank 14 is reduced to meet the discharge requirement, namely, after the pH value reaches the requirement, the flow direction of the slurry is switched by the switching valve 4, so that the slurry is discharged through the discharge pipe 5.|[0063] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.|[0064] Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.|[0065] In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; may be mechanically connected, may be electrically connected or may be in communication with each other; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.|[0066] In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.|[0067] For purposes of this disclosure, the terms "one embodiment," "some embodiments," "example," "a particular example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.|[0068] While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention. Family Number|(108940024)|108940024|Abstract|(CN117717989 A)|The invention provides a side aeration vortex type carbon sequestration and alkali reduction rapid reaction device which comprises a reaction tank , a stirring shell , a conveying pipe and an aeration pipe , the lower portion of the reaction tank is connected with the stirring shell , an impeller is arranged in the stirring shell , and the conveying pipe is connected with the stirring shell and connected with a backflow pipe and a discharging pipe through a switching valve . The aeration pipe is fixed on the side wall of the reaction tank , is positioned above the conical bottom shell and is connected with an exhaust port of the boiler through a gas conveying pipe . By arranging the stirring shell and the impeller , under the high - speed rotation effect of the impeller , slurry has a shearing and crushing effect on high - alkali solid waste , the specific surface area of a reaction molecular group is increased , alkaline substances in the high - alkali solid waste are rapidly separated out and fully dissolved in water , the phenomenon of ash in water is eliminated , solid - liquid mixing is more sufficient , and the reaction efficiency is improved ; the aeration pipe can be prevented from being blocked , and the slurry can circularly flow in the reaction tank , so that the generation of precipitates is prevented . |IPC codes|(CN117717989 A)|B01J - 004/00 |B01J - 019/00 |B01J - 019/18 |Title|(CN117717989 A)|Lateral aeration vortex type carbon sequestration and alkali reduction rapid reaction device | Chemical engineering B01J-004/00|B01J-019/00|B01J-019/18 B01J-004/00|B01J-019/00|B01J-019/18 CN117655070 CN117655070 108802945 WHO=Examiner SELF=Y CAT=L PENDING (CN117717989)|PENDING ALIVE (CN117717989)|ALIVE (CN117717989)|LEGAL DETAILS FOR CN117717989|Actual or expected expiration date=2043-12-07|Legal state=ALIVE|Status=PENDING|Event publication date=2023-12-07|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202311676996|Application date=2023-12-07|Standardized application number=2023CN-1676996|Event publication date=2024-03-19|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN117717989|Publication stage code=A|Publication date=2024-03-19|Standardized publication number=CN117717989|Event publication date=2024-03-19|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-04-05|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN117717989)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSZNVt6E6h85lfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000071811016&ekey=2394&xpn=CN117717989&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=XRor2AA5ycb02QeXYwSx7ZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN117717989)|CN (CN117717989)|NAME=ZHEJIANG HANGZHOU DRILLING MACHINE MANUFACTORY CO. LTD. , COUNTRY=CN (CN117717989)|NAME=TIAN NING;TSINGYIHUA INTELLECTUAL PROPERTY LLC , REG=11201 (CN117717989)|NAME=ZHU HUAJUN|NAME=YIN XIWEN|NAME=GAO LINJUN|NAME=LI YONGEN|NAME=DING XUHAI|NAME=GAN ZHICHAO|NAME=CHEN LI|NAME=YU QIUGE|NAME=DUAN ZHONGWEI|NAME=LIU GUI|NAME=XU GUODONG 0 1 Titre: (CN117717989)|Lateral aeration vortex type carbon sequestration and alkali reduction rapid reaction device Résumé: (CN117717989)|The invention provides a side aeration vortex type carbon sequestration and alkali reduction rapid reaction device which comprises a reaction tank, a stirring shell, a conveying pipe and an aeration pipe, the lower portion of the reaction tank is connected with the stirring shell, an impeller is arranged in the stirring shell, and the conveying pipe is connected with the stirring shell and connected with a backflow pipe and a discharging pipe through a switching valve. The aeration pipe is fixed on the side wall of the reaction tank, is positioned above the conical bottom shell and is connected with an exhaust port of the boiler through a gas conveying pipe. By arranging the stirring shell and the impeller, under the high-speed rotation effect of the impeller, slurry has a shearing and crushing effect on high-alkali solid waste, the specific surface area of a reaction molecular group is increased, alkaline substances in the high-alkali solid waste are rapidly separated out and fully dissolved in water, the phenomenon of ash in water is eliminated, solid-liquid mixing is more sufficient, and the reaction efficiency is improved; the aeration pipe can be prevented from being blocked, and the slurry can circularly flow in the reaction tank, so that the generation of precipitates is prevented. 16 Abstract gpt-4o-mini no The patent focuses on a device for carbon sequestration and alkali reduction but does not mention the accelerated weathering of silicate or alkaline minerals for CO₂ capture.
18 US63/293,689P|US63/293,689|US18/723,512|US63/414,191|US63/414,191P|WOCA2022/051893 WOCA2022/051893|IN202417047811|EP22908981|US18/723,512|BR112024012757|CN202280090809|CA3242169 EP4452871|US20250058273|IN202417047811|EP4452871|BR112024012757|CN118660865|BR112024012757|CA3242169|WO2023/115224 105522431 WO2023/115224 A1 2023-06-29 [WO2023115224]|IN202417047811 A 2024-12-20 [IN202417047811]|EP4452871 A4 2025-12-17 [EP4452871]|EP4452871 A1 2024-10-30 [EP4452871]|US20250058273 A1 2025-02-20 [US20250058273]|BR112024012757 A2 2024-09-17 [BR112024012757]|BR112024012757 A0 2024-07-02 [BR112024012757]|CN118660865 A 2024-09-17 [CN118660865]|CA3242169 A1 2023-06-29 [CA3242169] 2021-12-24|2022-10-07|2022-12-23 2022-12-23|2024-06-21|2022-12-23|2022-12-23|2022-12-23|2022-12-23|2022-12-23 2025-12-17|2025-02-20|2024-12-20|2024-10-30|2024-09-17|2024-09-17|2024-07-02|2023-06-29|2023-06-29 (EP4452871)|2042-12-23|(US20250058273)|2042-12-23|(WO2023/115224)|2025-06-24|(CN118660865)|2042-12-23|(IN202417047811)|2042-12-23|(BR112024012757)|2042-12-23|(CA3242169)|2042-12-23 (EP4452871)|Methods of carbon dioxide removal in freshwater (EP4452871)|Methods for carbon dioxide removal in inland waters and increased delivery of alkalinity to oceans. Methods can include adding one or more alkaline materials to one or more addition sites in an amount effective to enable enhanced weathering to occur, leading to net carbon dioxide removal from the atmosphere. CARBON DIOXIDE|CARBONRUN CARBON DIOXIDE REMOVAL (EP4452871)|Carbonrun Carbon Dioxide Removal Limited|(EP4452871)|Carbonrun Carbon Dioxide Removal Limited ([CA])|(US20250058273)|CARBONRUN CARBON DIOXIDE REMOVAL LIMITED ([CA])|(WO2023/115224)|CARBONRUN CARBON DIOXIDE REMOVAL LIMITED ([CA])|(CN118660865)|CARBON DIOXIDE LTD. ([CA])|(IN202417047811)|CARBONRUN CARBON DIOXIDE REMOVAL LIMITED|(BR112024012757)|LIMITED CARBONRUN CARBON DIOXIDE REMOVAL ([CA])||(CA3242169)|CARBONRUN CARBON DIOXIDE REMOVAL LIMITED ([CA]) STERLING SHANNON|HALFYARD EDMUND A (EP4452871)|STERLING, Shannon|HALFYARD, Edmund A.|(EP4452871)|STERLING, Shannon|HALFYARD, Edmund A. (EP4452871)|Dehns;St. Bride's House ([GB])|Reg. Nb: 101728904|(WO2023/115224)|BERESKIN & PARR LLP/S.E.N.C.R.L., S.R.L. ([CA])|(CN118660865)|ZHANG ZHENGZHENG;CHINA PAT INTELLECTUAL PROPERTY OFFICE|Reg. Nb: 11270|LI XUE;CHINA PAT INTELLECTUAL PROPERTY OFFICE|Reg. Nb: 11270|(CA3242169)|SMART & BIGGAR LP ([CA])|Reg. Nb: 2800 (US20250058273)|Examples of locating the treatment site at the outflow of the reactor include estuaries with high alkalinity, weathering reactions taking place inside a reactor, with high target inland waterbody discharge such that it is difficult to detect a change in concentration of carbon variables, or in other cases where it is difficult to detect a change in concentration of carbon variables.|In some embodiments, the alkaline material to be used is selected based on at least one of the following characteristics/considerations: the proximity to the source of the one or more alkaline materials, local availability, the cost of the one or more alkaline materials, an opportunity to reuse waste materials, the absence of impurities, toxins, heavy metals or other undesirable attributes, the ability to provide ecosystem co-benefits, such as the addition of calcium and magnesium in inland waters deficient in these elements, ability to optimize the introduction of alkalinity and increased pH when dissolved in freshwater, ability to optimize the speed of reaction within acceptable environmental limits.|In some embodiments, the reactor can be used when quantification of change in carbon variables is not possible downstream due to high levels of dilution (large target inland waterbody), or high background levels of the carbon variables exist in the receiving waters such that a change due to the addition is difficult to detect.| (US20250058273)|1. A method of removing atmospheric carbon dioxide (CO2), the method comprising: identifying a target inland waterbody having connectivity to an ocean; selecting one or more alkaline materials to be used; locating one or more addition sites in the target inland waterbody; establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; and adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody.|96. A method, comprising: identifying a target inland waterbody having connectivity to an ocean; selecting one or more alkaline materials to be used; locating one or more addition sites in the target inland waterbody; establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; and adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody, wherein the one or more methods of adding the one or more alkaline materials at the one or more addition sites comprises using alkaline amendment application infrastructure, wherein the alkaline amendment application infrastructure comprises a reactor, and wherein the reactor comprises a flue gas link to add concentrated CO2 to a reaction that takes place in the reactor.|97. A method, comprising: identifying a target inland waterbody having connectivity to an ocean; selecting one or more alkaline materials to be used; locating one or more addition sites in the target inland waterbody; establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody; and calculating carbon capture by estimating the amount of CO2 removal from the addition of the one or more alkaline materials to the target inland waterbody, wherein the amount of CO2 drawdown is estimated from increased carbonation weathering, increased alkalinity, or a combination thereof, and wherein the estimating the amount of CO2 drawdown (CDR) is obtained from the one or more treatment sites, treatment monitoring sites, control sites, estimation of baseline values, or any combination thereof.| (US20250058273)|Methods for carbon dioxide removal in inland waters and increased delivery of alkalinity to oceans. Methods can include adding one or more alkaline materials to one or more addition sites in an amount effective to enable enhanced weathering to occur, leading to net carbon dioxide removal from the atmosphere.| (US20250058273)|TARGET INLAND WATER(100,177)|CARBON DIOXIDE REMOVAL(100,59)|CARBON DIOXIDE(100,18)|ATMOSPHERIC CARBON DIOXIDE(100,5)|FRESHWATER(100,4)|PRETREATMENT ALKALINITY STATUS(89,21)|ECOSYSTEM COBENEFIT(45,2)|ALKALINITY INTRODUCTION(42,1)|ALKALINE MATERIAL(40,138)|CARBON VARIABLE(40,51)|REACTOR(36,54)|CALCIUM RICH PLAGIOCLASE FELDSPAR(35,2)|ALKALINITY INCREASED DELIVERY(34,1)|ALKALINE AMENDMENT APPLICATION INFRASTRUCTURE(33,14)|AMENDMENT APPLICATION INFRASTRUCTURE(31,14)|CONNECTIVITY(30,15)|ADDITION SITE(29,81)|SEA(29,40)|TREATMENT SITE(27,32)|ATTRIBUTE(27,1)|TREATMENT MONITORING SITE(26,7)|BODY WATERSHED(25,11)|METAMORPHIC ROCK RICH(25,2)|ALKALINITY(23,40)|BASELINE CALCULATION(23,2)|CARBON CAPTURE CALCULATION(21,7)|INCREASED CARBONATION(21,7)|DRAWDOWN(21,5)|BICARBONATE MEASUREMENT(21,2)|ECOLOGICAL VARIABLE WATER VARIABLE(21,2)|MAGNESIUM RICH PYROXENE(21,2)|INCREASING ALKALINITY(20,9)|WEATHERING(20,8)|ESTUARY(20,5)|FLUE GAS LINK(20,3)|BASELINE VALUE(19,6)|CARBONATE ROCK(19,2)|CEMENT KILN DUST(18,3)|TOXIN(18,1)|TARGET INLAND WATER INTEREST(17,2)|GRAY EMISSION(16,12)|CARBONATION WEATHERING REACTION(16,5)|INCREASING DELIVERY(16,2)|INLAND WATER(15,28)|CARBON CAPTURE STRATEGY(15,19)|CARBON VARIABLE MEASUREMENT(15,2)|SPECIALIZED LIMING BARGE EMERSION(15,1)|WEATHERING ZONE(14,10)|CRUSHED DOLOMITIC LIMESTONE(14,2)|ENHANCED WEATHERING(13,4)|HELICOPTER(13,2)|WOLLASTONITE(13,2)|INLANDWEST RIVERNORTH RIVERWATERBODYB(13,1)|EXTRA ALKALINITY(12,5)|AIRPLANE(12,2)|BODY DISCHARGE(12,2)|DRONE(12,2)|NEIGHBORING HYDROMETRIC STATION(12,2)|OLIVINE(12,2)|LARGE TARGET INLAND WATER(12,1)|CARBONATE MINERAL(11,7)|QUARRY(11,3)|AUTOMATED LIME DOSER(11,2)|BASALT(11,2)|PRETREATMENT CONNECTIVITY STATUS(11,2)|CARBONATION WEATHERING STOICHIOMETRY(11,1)|CALCITE(10,3)|HEADWATER LAKE(10,3)|ECOLOGICAL COBENEFIT(10,2)|FLOOD PLAIN BOUNDARY(10,2)|INCREASING PH(10,2)|LAKE LIMNOLOGICAL CHARACTERIZATION(10,1)|BOAT(9,10)|DAM(9,8)|FLUE GAS(9,6)|ALKALINE AMENDMENT MASS(9,3)|ANTHROPOGENIC IMPACT(9,3)|POND(9,3)|NEIGHBORING WATERSHED(9,2)|TRUCK(9,2)|DOLOMITE ALKALINE AMENDMENT(9,1)|ORGANIZATION GHG INVENTORY(9,1)|IDENTIFIED TARGET INLAND WATER(8,6)|CEMENT PLANT(8,3)|ATLANTIC SALMON POPULATION(8,2)|CONVEYER BELT(8,2)|LOGISTICAL RESOURCE(8,2)|RIVER DRAINAGE NETWORK SLOPE(8,2)|ALKALINE AMENDMENT STRATEGY(8,1)|BICARBONATE EXPORT FLUX(8,1)|CARBONATION STOICHIOMETRY(8,1)|CHANNEL FLUVIAL GEOMORPHOLOGY STRAIGHTNESS(8,1)|ESTABLISHED PRETREATMENT ALKALINITY STATUS(8,1)|INDIRECT GHG EMISSION(8,1)|WATERSHED HYDROLOGY(8,1)|AVERAGE GRAIN SIZE(7,5)|NON CARBONATE ALKALINE AMENDMENT(7,4)|STORAGE SILO(7,3)|LAND ENHANCED WEATHERING PROJECT(7,2)|ROVING STATION(7,2)|ACIDIC RIVERALKALINE NEUTRAL RIVER(7,1)|ALKALINE AMENDMENT DELIVERY(7,1)|ALKALINE AMENDMENT DOSAGE(7,1)|AMBIENT ALKALINITY DISCRETE ESTIMATE(7,1)|FUEL COMBUSTION ONSITE(7,1)|MINERAL ALKALINE AMENDMENT(7,1)|PRETREATING RIVERNONE(7,1)|WATERCRAFT GUNNEL(7,1)|DRAWDOWN REMOVAL(6,14)|CARBON DRAWDOWN(6,3)|CALCIUM OXIDE(6,2)|CARBONATE ANION(6,2)|MEAN ANNUAL DISCHARGE(6,2)|MICROBIAL CATALYST(6,2)|PROJECT ORGANIZATION(6,2)|REACTOR INTRODUCTION(6,2)|WATER ALKALINITY STATUS(6,2)|WATERSHED MODEL(6,2)|WETLAND DISTRIBUTION(6,2)|CACO PRECIPITATION(6,1)|DISCONNECTED CONNECTIVITY(6,1)|DOLOMITE AMENDMENT(6,1)|ECOSYSTEM HEALTH(6,1)|ESTUARY RIVER MOUTH(6,1)|EXPERIMENTAL INFRASTRUCTURE(6,1)|GRANITE BEDROCK(6,1)|INLAND WATER PREALKALINITY STATUS(6,1)|KILLAG RIVER(6,1)|MICROBIAL AMENDMENT(6,1)|PEATLAND WETLAND PROPORTION(6,1)|PYRITIC SLATE(6,1)|RESIDENCY PROLONGATION(6,1)|RIVER ACIDIFICATION(6,1)|STRATIFICATION SCHEDULE(6,1)|SUSPENDED SEDIMENT ESTHETIC CONCERN(6,1)|TARGET WATERSHED PH(6,1)|TURNOVER REGIME(6,1)|UNDERWATER TERRAIN(6,1)|PCO(5,7)|ALKALINE EARTH METAL(5,4)|EVASION(5,4)|ACID NEUTRALIZATION(5,2)|CARBON VARIABLE TARGET RANGE(5,2)|HEAVY METAL(5,2)|LABORATORY ANALYSIS(5,2)|OUTSIDE CARBONATION(5,2)|TRANSITION ALKALINITY WATER(5,2)|ALKALINE DISSOLUTION(5,1)|ALKALINE MINERAL EXPOSURE(5,1)|ALKALINITY STATUS TREATMENT(5,1)|AQUEOUS ENVIRONMENT SALINITY(5,1)|BASELINE CONDITION FUTURE PREDICTION(5,1)|BASELINE SCENARIO(5,1)|BIOGEOCHEMICAL MODEL(5,1)|CARBONATION WEATHERING RATE(5,1)|COARSE GRAVEL(5,1)|CUMULATIVE DAILY(5,1)|DAILY TIMESTEP(5,1)|DEPLOYING SILICATE(5,1)|DOSING ALGORITHM VARIABLE(5,1)|ECOLOGICAL CONCERN(5,1)|ENTRAINMENT THRESHOLD(5,1)|FINAL ALKALINE AMENDMENT(5,1)|HCO DELIVERY(5,1)|HCO RETENTION(5,1)|LAKE BASIN(5,1)|MODEL ESTABLISHED PRETREATMENT(5,1)|NET ECOSYSTEM PRODUCTION(5,1)|PLANNED ENHANCED WEATHERING PROJECT(5,1)|PRECISE CARBONATION(5,1)|RIVER STAGEG AA(5,1)|SNOWPACK MELT(5,1)|UPSTREAM DOSER(5,1)|WASTE MATERIAL(5,1)|WATERSHED BOUNDARY(5,1)|WATERSHED INTEREST(5,1)|WATERSHED REACH(5,1)|CARBONATION WEATHERING(4,7)|TARGET VALUE(4,5)|ALKALINITY ADDITION(4,3)|DRY POWDER(4,3)|ECOLOGY(4,3)|KGPH TPH BM(4,3)|TURBULENCE(4,3)|TURBULENT WATER(4,3)|ALKALI METAL(4,2)|INDUSTRIALLY PRODUCED ALKALINE MATERIAL(4,2)|ALKALINE REAGENT(4,1)|ALKALINITY GENERATION(4,1)|ANIONIC SPECIES(4,1)|BICARBONATE DELIVERY(4,1)|BICARBONATE FLUX(4,1)|DISCHARGE REGIME STABILITY(4,1)|DOWNSTREAM MONITORING SITE(4,1)|ESTIMATING RIVER DISCHARGE(4,1)|FINE GRAINSIZE(4,1)|INCREASED OCEAN ALKALINITY(4,1)|INORGANIC CARBON SPECIES SUM(4,1)|LASTING ENVIRONMENTAL HARM(4,1)|OUTFLOW CONDUIT(4,1)|PARTICULATE INORGANIC CARBON(4,1)|REACTANT GAS(4,1)|REACTANT TRANSPORT MODEL(4,1)|RIVER GRADIENT(4,1)|SENSOR ASSEMBLAGE(4,1)|SHALLOW GRADIENT(4,1)|SPECIES POPULATION(4,1)|STABLE DISCHARGE REGIME(4,1)|STRONG ACID IMPAIRED CARBONATION(4,1)|TARGET INLAND WATER CARBONATE(4,1)|TOOL PROTECTION(4,1)|TRANSPORTATION NETWORK(4,1)|UNSTATED FEATURE(4,1)|WEATHERING RATE ITERATIVE MEASUREMENT(4,1)|CARBONIC ACID(3,4)|CLAY(3,4)|PATHWAY(3,4)|ROAD NETWORK(3,4)|CIHCO(3,3)|SLURRY(3,3)|ACCESSIBILITY(3,2)|ALKALINE AMENDMENT ADDITION INFRASTRUCTURE(3,2)|CONTAMINANT(3,2)|DEVIATION(3,2)|DOSING RATE(3,2)|DRAINAGE WATER(3,2)|GROUNDWATER(3,2)|IMPOUNDMENT(3,2)|INCREASED TURBIDITY(3,2)|MEAN PH(3,2)|ACHIEVEDCDR REMAINS(3,1)|ADDING DOLOMITEH(3,1)|ALKALI TREATMENT(3,1)|ALKALINITY INPUT(3,1)|ANDUPSTREAM CONTROLUPSTREAM CONTROL(3,1)|BICARBONATE CONCENTRATION DIFFERENCE(3,1)|CARBON CAPTURE CALCULATION ESTIMATE(3,1)|CHANNEL RAINFALL(3,1)|CONDUCTIVITY SENSOR(3,1)|DOLOMITE ADDITION SITE CRUSHEDDIRECT(3,1)|DOWNSTREAM SENSOR(3,1)|FIXED STATION(3,1)|FLUX SENSOR(3,1)|FREQUENT CYCLE(3,1)|FULL DISSOLUTION(3,1)|GATHER INFORMATION(3,1)|HCO INCREASED DELIVERY(3,1)|HCO LOSS(3,1)|HYDROLOGICAL DISCHARGE RATE(3,1)|INLAND WATERWAY(3,1)|INTERESTCO PERIOD(3,1)|LOWERMOST REACH(3,1)|MAINTENANCE VEHICLE(3,1)|MASS SUM(3,1)|NONLINEAR RELATION(3,1)|NUTRIENT(3,1)|PERIODIC MEASUREMENT(3,1)|PRETREATMENT PHASE(3,1)|PRETREATMENT RELATION(3,1)|REDUCED OCEAN ACIDIFICATION(3,1)|REDUCTION TOXIC IONIC ALUMINUM(3,1)|RIVER MOUTH TREATMENT SITE(3,1)|RIVER NATURE(3,1)|STATISTICAL RELATION(3,1)|STOCHASTIC RELATION(3,1)|STREAM AGITATION(3,1)|TARGET ZONE(3,1)|TREATMENT MONITORING STATION(3,1)|STUDY PERIOD(2,9)|CONTROL SITE(2,5)|3CDR GROSS(2,1)|ACCOUNTING(2,1)|ACID ANION(2,1)|ADDITIONALNON CARBONATE ALKALINE MATERIAL(2,1)|ALGAL BLOOM(2,1)|ALKALINE MATERIAL GRAINSIZE(2,1)|ALKALINE MATERIAL TODOSER(2,1)|ALKALINE PRODUCT(2,1)|ANTHROPOGENIC WATER INPUT(2,1)|AUTOMATION(2,1)|BIODIVERSITY(2,1)|BODY CHEMISTRY(2,1)|BYPRODUCT(2,1)|CA INCREASE(2,1)|CARBON MODEL(2,1)|CARBON MONITORING(2,1)|CARBONATE SATURATION CONCENTRATION(2,1)|CARBONATE STOICHIOMETRIC RATIO(2,1)|CLOSED REACTOR(2,1)|CONCENTRATION SENSOR(2,1)|DAILY MONTHLY(2,1)|DATA MODEL(2,1)||(WO2023/115224)|CARBON DIOXIDE REMOVAL(100,66)|CO2(100,38)|PRETREATMENT ALKALINITY STATUS(100,31)|CARBON DIOXIDE(100,30)|ATMOSPHERIC CARBON DIOXIDE(100,8)|FRESHWATER(100,5)|TARGET INLAND WATER(88,207)|NONCARBONATE ALKALINE AMENDMENT(41,1)|FRESHWATER RIVER(39,1)|ACCELERATED CARBONATION(37,1)|ECOSYSTEM COBENEFIT(35,2)|CARBON PEAK(34,30)|ALKALINITY INTRODUCTION(33,1)|ALKALINE MATERIAL(32,154)|ALKALINITY(29,45)|CARBON CAPTURE STRATEGY(29,26)|CARBON VARIABLE(27,26)|CONNECTIVITY(27,19)|ESTABLISHED PRETREATMENT ALKALINITY STATUS(27,2)|RIVER MOUTH(26,51)|REACTOR(25,54)|GATE RICH PLAGIOCLASE FELDSPAR(25,2)|BODY WATERSHED(23,12)|INCREASED CARBONATION(23,10)|ECOLOGICAL PEAK VALUE(23,2)|SEA(22,51)|TREATMENT SITE(22,44)|ALKALINE AMENDMENT APPLICATION INFRASTRUCTURE(21,14)|ATTRIBUTE(21,1)|ADDITION SITE(20,90)|MEAN PH(20,6)|WATERSHED BOUNDARY(20,2)|INCREASING ALKALINITY(19,11)|METAMORPHIC ROCK RICH(19,2)|CARBON DIOXIDE DRAWDOWN(19,1)|FRESHWATER LAKE(19,1)|INLAND WATER(18,34)|BASELINE CALCULATION(18,2)|ANTHROPOGENIC IMPACT(17,4)|BICARBONATE MEASUREMENT(17,2)|ECOLOGICAL VARIABLE WATER VARIABLE(17,2)|ALKALINITY INCREASED DELIVERY(17,1)|WEATHERING(16,9)|WETLAND(16,4)|MAGNESIUM RICH PYROXENE(16,2)|ESTUARY(15,5)|CARBONATE ROCK(15,2)|GRAY EMISSION(14,15)|RIVER(14,12)|CEMENT KILN DUST(14,3)|TOXIN(14,1)|WEATHERING ZONE(13,14)|TURBULENT WATER(13,5)|CONCENTRATED CO2(13,4)|STATISTICAL RELATION(13,2)|TARGET INLAND WATER INTEREST(13,2)|BARGE(12,11)|TREATMENT MONITORING SITE(12,8)|WATER PEAK(12,6)|CARBONATION WEATHERING REACTION(12,5)|LAKE(11,8)|CRUSHED DOLOMITIC LIMESTONE(11,2)|BOAT(10,11)|PCO(10,9)|AIRPLANE(10,2)|HELICOPTER(10,2)|NEIGHBORING HYDROMETRIC STATION(10,2)|WOLLASTONITE(10,2)|INCREASING PH(10,1)|CARBONATE MINERAL(9,7)|CARBON CAPTURE CALCULATION(9,6)|DRY POWDER(9,4)|MICROBIAL COMMUNITY(9,3)|QUARRY(9,3)|BASALT(9,2)|BODY DISCHARGE(9,2)|DRONE(9,2)|NEUTRALIZING STRONG ACID(9,2)|OLIVINE(9,2)|PRECIPITATION(9,2)|PRETREATMENT CONNECTIVITY STATUS(9,2)|RIVER WATER(9,2)|SNOWMELT(9,2)|CARBONATION WEATHERING STOICHIOMETRY(9,1)|LARGE TARGET INLAND WATER(9,1)|AVERAGE GRAIN SIZE(8,6)|BASELINE VALUE(8,6)|WEST RIVER(8,6)|ECOLOGY(8,4)|CALCITE(8,3)|FLOOD PLAIN BOUNDARY(8,2)|FLUE GAS LINK(8,2)|FLUVIAL GEOMORPHOLOGY(8,2)|INCREASING DELIVERY(8,2)|GATE ADDITION(8,1)|DAM(7,8)|LAND ENHANCED WEATHERING PROJECT(7,3)|POND(7,3)|ATLANTIC SALMON POPULATION(7,2)|CONVEYER BELT(7,2)|DRAINAGE NETWORK CONFIGURATION(7,2)|HEADWATER LAKE(7,2)|LOGISTICAL RESOURCE(7,2)|NEIGHBORING WATERSHED(7,2)|RIVER DRAINAGE NETWORK SLOPE(7,2)|SATURATION LEVEL(7,2)|TRUCK(7,2)|ESTIMATING CO2 DRAWDOWN(7,1)|ORGANIZATION GHG INVENTORY(7,1)|IDENTIFIED TARGET INLAND WATER(6,6)|PATHWAY(6,5)|SLURRY(6,4)|ACIDIC RIVER(6,3)|CARBONATE ANION(6,3)|CEMENT PLANT(6,3)|HCOS DELIVERY(6,3)|ALKALINE AMENDMENT MASS(6,2)|CO2 EVASION REDUCTION(6,2)|PLANNED ENHANCED WEATHERING PROJECT(6,2)|REYNOLD NUMBER(6,2)|SEQUESTERING CO2(6,2)|ALKALINE AMENDMENT STRATEGY(6,1)|ALKALINE MATERIAL DOSING RATE(6,1)|AUTOMATED LIME DOSER(6,1)|BICARBONATE EXPORT FLUX(6,1)|CARBONATION STOICHIOMETRY(6,1)|INDIRECT GHG EMISSION(6,1)|WATERSHED HYDROLOGY(6,1)|FIXED STATION(5,4)|STORAGE SILO(5,3)|ALKALINITY GENERATION(5,2)|BASELINE SCENARIO(5,2)|CALCIUM OXIDE(5,2)|MEAN ANNUAL DISCHARGE(5,2)|MICROBIAL CATALYST(5,2)|PROJECT ORGANIZATION(5,2)|REACTOR INTRODUCTION(5,2)|WATER ALKALINITY STATUS(5,2)|WATERSHED MODEL(5,2)|WETLAND DISTRIBUTION(5,2)|ALKALINE AMENDMENT DELIVERY(5,1)|ALKALINE AMENDMENT DOSAGE(5,1)|AMBIENT ALKALINITY DISCRETE ESTIMATE(5,1)|CARBON DIOXIDE VALUE(5,1)|FUEL COMBUSTION ONSITE(5,1)|KILLAG RIVER SITE(5,1)|LIMNOLOGICAL CHARACTERIZATION(5,1)|PULVERIZED ALKALINE MINERAL(5,1)|REAGENT(4,5)|ALKALINE EARTH METAL(4,4)|CONTINUOUS MONITORING PERMANENT STATION(4,4)|CO2 DISSOLUTION(4,3)|NON CARBONATE ALKALINE AMENDMENT(4,3)|ACID NEUTRALIZATION(4,2)|CACOS(4,2)|CARBON DRAWDOWN(4,2)|CARBON VARIABLE TARGET RANGE(4,2)|HEAVY METAL(4,2)|LABORATORY ANALYSIS(4,2)|TRANSITION ALKALINITY WATER(4,2)|WATER SLOPE(4,2)|ALKALINE DISSOLUTION(4,1)|ALKALINE MINERAL EXPOSURE(4,1)|AQUATIC DELIVERY CONDUIT BREAKDOWN(4,1)|AQUEOUS ENVIRONMENT SALINITY(4,1)|BASELINE CONDITION FUTURE PREDICTION(4,1)|BASELINE PROJECTION(4,1)|BIOGEOCHEMICAL MODEL(4,1)|CARBONATION WEATHERING RATE(4,1)|COARSE GRAVEL(4,1)|CUMULATIVE DAILY(4,1)|DAILY TIMESTEP(4,1)|DEPLOYING SILICATE(4,1)|DOCUMENT ECOSYSTEM(4,1)|DOLOMITE AMENDMENT(4,1)|DOSING ALGORITHM VARIABLE(4,1)|DRAINAGE NETWORK ALKALINITY STATUS(4,1)|ECOLOGICAL CONCERN(4,1)|ECOSYSTEM HEALTH(4,1)|ENTRAINMENT THRESHOLD(4,1)|ESTUARY RIVER MOUTH(4,1)|FINAL ALKALINE AMENDMENT(4,1)|FORESTED LAND(4,1)|GRANITE BEDROCK(4,1)|H2CO PROPORTION(4,1)|MINERAL WEATHERING(4,1)|MODEL ESTABLISHED PRETREATMENT(4,1)|MODIFIED ALKALINE AMENDMENT(4,1)|NET ECOSYSTEM PRODUCTION(4,1)|PMOL RRR2S(4,1)|POWDERED LIMESTONE(4,1)|PRECISE CARBONATION(4,1)|RESIDENCY PROLONGATION(4,1)|SUSPENDED SEDIMENT ESTHETIC CONCERN(4,1)|TARGET WATERSHED PH(4,1)|TURNOVER REGIME(4,1)|UNDERWATER TERRAIN(4,1)|WASTE MATERIAL(4,1)|WATERSHED INTEREST(4,1)|WATERSHED REACH(4,1)|CARBONATION WEATHERING(3,7)|GROSS(3,6)|CARBONIC ACID(3,5)|TARGET VALUE(3,5)|BROAD REGION(3,3)|STRATIFICATION(3,3)|ACCESSIBILITY(3,2)|ALKALI METAL(3,2)|ALKALINE AMENDMENT ADDITION INFRASTRUCTURE(3,2)|CONTAMINANT(3,2)|DRAINAGE WATER(3,2)|FLOW VELOCITY(3,2)|GROUNDWATER(3,2)|IMPOUNDMENT(3,2)|INCREASED TURBIDITY(3,2)|INDUSTRIALLY PRODUCED ALKALINE MATERIAL(3,2)|TURBULENCE(3,2)|WATER DISCHARGE(3,2)|ALKALINITY ADDITION ECOLOGICAL COBENEFIT(3,1)|AMENDMENT INCREASED CO2 EMISSION(3,1)|ANIONIC SPECIES(3,1)|AVERAGE CO2 FLUX(3,1)|BICARBONATE DELIVERY(3,1)|BICARBONATE FLUX(3,1)|BODY LIME DOSER(3,1)|CARBONATE SILICATE CYCLE(3,1)|CHANNEL STRAIGHTNESS(3,1)|CO2 CARBON SPECIES(3,1)|CO2 MEASUREMENT(3,1)|DISCHARGE REGIME STABILITY(3,1)|EARTH HISTORY(3,1)|ESTIMATE CO2(3,1)|FINE GRAINSIZE(3,1)|GLOBAL BIOGEOCHEMICAL CYCLE(3,1)|HCOS SHOW MEASUREMENT(3,1)|INCREASED ALKALINITY STRATEGY(3,1)|INCREASED OCEAN ALKALINITY(3,1)|INORGANIC CARBON SPECIES SUM(3,1)|LASTING ENVIRONMENTAL HARM(3,1)|LEADERSHIP GHG INVENTORY DEVELOPMENT(3,1)|MINERAL SOIL HORIZON(3,1)|NATURAL WEATHERING REACTION(3,1)|OUTFLOW CONDUIT(3,1)|PARTICULATE INORGANIC CARBON(3,1)|PRETREATMENT COLLECTION(3,1)|REACTANT GAS(3,1)|REACTANT TRANSPORT MODEL(3,1)|RELEASING CO2(3,1)|RIVER GRADIENT(3,1)|ROCK DISPERSION(3,1)|SHALLOW GRADIENT(3,1)|SPECIES POPULATION(3,1)|STABLE DISCHARGE REGIME(3,1)|STRONG ACID IMPAIRED CARBONATION(3,1)|TARGET INLAND WATER CARBONATE(3,1)|TOOL PROTECTION(3,1)|TRANSPORTATION NETWORK(3,1)|UNSTATED FEATURE(3,1)|UPTAKE CO2(3,1)|WATER DELIVERY CONDUIT(3,1)|WEATHERING RATE ITERATIVE MEASUREMENT(3,1)|STUDY PERIOD(2,9)|CLAY(2,4)|OCEAN ALKALINITY ENHANCEMENT(2,4)|ROAD NETWORK(2,4)|SHOW CO2(2,3)|TCO2E(2,3)|DEVIATION(2,2)|ACCOUNTING(2,1)|ACID ANION(2,1)|ALGAL BLOOM(2,1)|ALKALI TREATMENT(2,1)|ALKALINE MATERIAL GRAINSIZE(2,1)|ALKALINE MATERIAL KINETICS(2,1)|ALKALINE NEUTRAL RIVER(2,1)|ALKALINE PRODUCT(2,1)|ALKALINITY STATUS FUNCTION(2,1)|ANTHROPOGENIC WATER INPUT(2,1)|BATHYMETRIC DATA(2,1)|BICARBONATE CONCENTRATION DIFFERENCE(2,1)|BIODIVERSITY(2,1)|BODY CHEMISTRY(2,1)|BYPRODUCT(2,1)|CHANNEL RAINFALL(2,1)|CO2 DRAWDOWN REMOVAL(2,1)|CO2 MASS(2,1)|CO2 POTENTIAL LOSS(2,1)|CO2 REMOVAL DRAWDOWN(2,1)|DATA COLLECTED PRETREATMENT(2,1)|DISSOLUTION REACTION(2,1)|DOWNSTREAM SENSOR(2,1)|DOWNSTREAM TREATMENT SITE(2,1)|FREQUENT CYCLE(2,1)|FULL DISSOLUTION(2,1)|GASEOUS ENVIRONMENT(2,1)|GATHER INFORMATION(2,1)|GLACIAL MASS(2,1)|GLOBAL WARMING REDUCTION(2,1)|HCOS LOSS(2,1)|HYDROLOGICAL DISCHARGE RATE(2,1)|INLAND WATER ALKALINITY(2,1)|INLAND WATERWAY(2,1)|LONGTERM STORAGE(2,1)|LOWERMOST REACH(2,1)|MAINTENANCE VEHICLE(2,1)|MASS SUM(2,1)|MONITORING STATION(2,1)|NET CO2 REMOVAL(2,1)|NONLINEAR RELATION(2,1)|NUTRIENT(2,1)|PERIODIC MEASUREMENT(2,1)|PRETREATMENT PHASE(2,1)|PRETREATMENT RELATION(2,1)|REDUCED OCEAN ACIDIFICATION(2,1)|REDUCTION TOXIC IONIC ALUMINUM(2,1)|RIVER MOUTH TREATMENT SITE(2,1)|RIVER NATURE(2,1)|STABLE BICARBONATE(2,1)|STOCHASTIC RELATION(2,1)|STREAM AGITATION(2,1)|TARGET ZONE(2,1)||(CN118660865)|PRETREATMENT ALKALINITY(100,29)|CARBON DIOXIDE(100,27)|ATMOSPHERIC CARBON DIOXIDE(100,7)|FRESH WATER(100,4)|REMOVING CARBON DIOXIDE(100,1)|TARGET INLAND WATER(67,179)|FRESHWATER RIVER(44,1)|ACCELERATED CARBONATION(42,1)|CARBON VARIABLE(39,49)|TARGET INLAND(38,17)|ALKALINE MATERIAL(37,148)|ALKALINITY INTRODUCTION(37,1)|ESTUARY(35,55)|ECOLOGICAL BENEFIT(35,1)|ALKALINITY(33,65)|SEA(29,55)|WATER TARGET INLAND(29,13)|REACTOR(28,58)|ADDITION SITE(24,92)|ATTRIBUTE(24,1)|ECOSYSTEM COMMON BENEFIT(24,1)|INCREASED CARBONATION EFFLORESCENCE(24,1)|AVERAGE PH(23,6)|INCREASING ALKALINITY(23,3)|TREATMENT SITE(22,44)|METAMORPHIC ROCK RICH(22,2)|PYROXENE RICH(21,2)|FRESHWATER LAKE(21,1)|ALKALINE MODIFIER APPLICATION INFRASTRUCTURE(20,14)|TARGET INLAND WATER BASIN(20,4)|SNOW MELTING(20,1)|ECOLOGICAL VARIABLE VALUE(19,9)|WATER DELIVERY PIPE(19,1)|TRANSITION ALKALINITY(18,4)|WETLAND(18,4)|BASIN BOUNDARY(18,2)|BERTAGNI(18,1)|INCREASED ALKALINITY DELIVERY(18,1)|RIVER(17,16)|TURBULENT WATER(17,3)|CARBONATE ROCK(17,2)|HYDRAULIC DIP(17,2)|HORGBBY(17,1)|CEMENT KILN DUST(16,3)|DILUTION LEVEL(16,1)|ESTIMATED BASELINE VALUE(16,1)|EVIDENCE(16,1)|TOXIN(16,1)|INLAND WATER(15,39)|GRAY EMISSION(15,15)|REDUCING CARBON DIOXIDE(15,2)|BODY BASIN(14,5)|CARBON CAPTURE STRATEGY DEVELOPMENT(14,2)|STATISTICAL RELATIONSHIP(14,2)|TREATMENT MONITORING SITE(13,8)|BARGE(12,11)|DAM(12,9)|LAKE(12,8)|TRANSITIONAL ALKALINITY(12,4)|AGITATION(12,3)|CRUSHED DOLOMITE LIMESTONE(12,2)|INCREASING PH(12,1)|WEATHERED ZONE(11,6)|BOAT(11,5)|SUSPENDED SEDIMENT(11,5)|NON CARBONATE ALKALINE MODIFIER(11,4)|MICROBIAL COMMUNITY(11,3)|ANORTHITE(11,2)|ARTIFICIAL WATERWAY(11,2)|DISCONNECTION(11,2)|HELICOPTER(11,2)|STORAGE BIN(11,2)|WOLLASTONITE(11,2)|AIRCRAFT(11,1)|CARBON VARIABLE VALUE(10,8)|CARBONATE MINERAL(10,7)|CARBON CAPTURE CALCULATION(10,6)|DRY POWDER(10,4)|MARINE ALKALINITY(10,3)|PH VALUE(10,3)|QUARRY(10,3)|BASALT(10,2)|DIRECTLY MEASURING BICARBONATE(10,2)|DRONE(10,2)|ECOLOGY(10,2)|ENDANGERED SPECIES(10,2)|ESTABLISHED TARGET INLAND WATER(10,2)|OLIVINE(10,2)|PRECIPITATION(10,2)|RIVER WATER(10,2)|AVERAGE PARTICLE SIZE(9,6)|WEST RIVER(9,6)|CALCITE(9,3)|HCO INCREMENT(9,3)|ARTIFACT INVESTIGATION(9,2)|AUTOMATIC LIME DOSER(9,2)|CARBONATE ALKALINE IMPROVER(9,2)|ECOLOGICAL COBENEFIT(9,2)|PRETREATED ALKALINITY(9,2)|RIVER DRAINAGE NETWORK DIP(9,2)|FEATURE CONSIDERATION(9,1)|USEPA GHG INVENTORY DEVELOPMENT(9,1)|POND(8,3)|DRAINAGE NETWORK CONFIGURATION(8,2)|LOGISTICAL RESOURCE(8,2)|SATURATION LEVEL(8,2)|TRUCK(8,2)|LARGE TARGET INLAND WATER(8,1)|ORGANIZATION GHG INVENTORY(8,1)|CARBON VALUE VARIANCE(7,4)|SLURRY(7,4)|ACIDIC RIVER(7,3)|CEMENT PLANT(7,3)|ATLANTIC SALMON POPULATION(7,2)|CONVEYER BELT(7,2)|DOMAIN(7,2)|ECOLOGICAL INVESTIGATION(7,2)|STATISTICAL MODEL(7,2)|ALKALINITY DISCRETE ESTIMATE(7,1)|CARBONATION STOICHIOMETRY(7,1)|CENTRALIZED OFFSITE MONITORING STATION(7,1)|DOLOMITE ALKALINE MODIFIER(7,1)|INCREMENTAL HCO TRANSPORT(7,1)|INDIRECT GHG EMISSION(7,1)|TOXIC MICROORGANISM ALGAE PROLIFERATION(7,1)|CARBON DIOXIDE REMOVAL(6,70)|ALKALINITY ADDITION(6,5)|CARBONATE ANION(6,3)|WATER INPUT(6,3)|DOLOMITE PURITY(6,2)|EFFLUENT CONTAMINATION(6,2)|LAND ENHANCED WEATHERING PROJECT(6,2)|LIME DOSING(6,2)|MODIFIED ALKALINE MODIFIER(6,2)|ALKALINE MODIFIER STRATEGY(6,1)|CARBONATED WEATHERING(6,1)|CARBONATION WEATHERING REACTION OCCURRENCE(6,1)|DROUGHT EXACERBATION(6,1)|ECOSYSTEM COBENEFIT(6,1)|GASEOUS REACTANT TRANSPORT(6,1)|HEAVY METAL(6,1)|LACUNARY CHARACTERIZATION(6,1)|POWDERED ALKALINE MINERAL(6,1)|PRECIPITATE ENTRAINMENT THRESHOLD(6,1)|RESIDENT OWNERSHIP(6,1)|RIVER BASIN HYDROLOGY(6,1)|SEDIMENT ENTRAINMENT(6,1)|SITE KILLAG RIVER(6,1)|STEADY EMISSION REGIME(6,1)|TCO(5,10)|COLLECT INFORMATION(5,5)|CALCIUM OXIDE(5,2)|FLUE GAS CONNECTION(5,2)|MAGNESIUM OXIDE(5,2)|MICROBIAL CATALYST(5,2)|PROJECT ORGANIZATION(5,2)|REACTOR EFFLUENT LOCATION(5,2)|WETLAND DISTRIBUTION(5,2)|ALKALINE MODIFIER DELIVERY(5,1)|ALKALINITY LOSS MITIGATION(5,1)|ASSIGNING ALKALINITY(5,1)|BASELINE SCENARIO(5,1)|DOLOMITE MODIFIER(5,1)|ECOSYSTEM HEALTH(5,1)|GRANITE BEDROCK(5,1)|INFIELD OBSERVATION(5,1)|MITIGATE RELIANCE(5,1)|NET ECOSYSTEM YIELD(5,1)|OCEAN ACIDIFICATION(5,1)|REACTION RATE(5,1)|SCOTCH PROVINCE BROAD REGION(5,1)|UNDERWATER TERRAIN(5,1)|WATER QUALITY LEVEL(5,1)|ALKALINE EARTH METAL(4,4)|IDENTIFIED TARGET INLAND WATER(4,4)|PERMANENT CONTINUOUS MONITORING STATION(4,4)|METRIC TON(4,3)|WATER VARIABLE VALUE(4,3)|ACID NEUTRALIZATION(4,2)|AUTOMATION(4,2)|BASIN MODEL(4,2)|BICARBONATE OUTPUT FLUX(4,2)|FLOOD ZONE BOUNDARY(4,2)|LABORATORY ANALYSIS(4,2)|RIVER REACH(4,2)|ACCURATE CARBONATION(4,1)|ADJACENT HYDROLOGIC OBSERVATORY(4,1)|ALKALI CATION(4,1)|ALKALINE MODIFIER MASS(4,1)|ALKALINE REAGENT(4,1)|ALKALINITY PRODUCTION(4,1)|ALKALINITY STATUS(4,1)|ANIONIC SPECIES(4,1)|ANNUAL AVERAGE DISCHARGE(4,1)|ANNUAL AVERAGE EMISSION(4,1)|AQUEOUS ENVIRONMENT SALINITY(4,1)|BICARBONATE DELIVERY(4,1)|BICARBONATE FLUX DIFFERENCE(4,1)|BIOELECTROCHEMICAL MODEL(4,1)|BIOTIC STRESS INDICATOR(4,1)|CARBONATE SILICATE CYCLE(4,1)|CDR CALCULATION(4,1)|COMMUNICATION PRECONDITION(4,1)|DELIVERY SCHEDULE(4,1)|DEPLOYING SILICATE MINERAL(4,1)|DOCUMENT PROTECTION(4,1)|DOSING ALGORITHM VARIABLE(4,1)|DOWNSTREAM ALKALINITY(4,1)|DOWNSTREAM TURBIDITY(4,1)|DRAINAGE STABILITY(4,1)|EARTH HISTORY(4,1)|ECOLOGICAL COMMUNITY BENEFIT(4,1)|ESTUARY SEGMENT(4,1)|ESTUARY TREATMENT SITE(4,1)|GLOBAL BIO GEOCHEMICAL CYCLE(4,1)|HCO MEASUREMENT(4,1)|HCO RETENTION(4,1)|INFERRING TREATMENT(4,1)|INTRODUCING ALKALINITY(4,1)|MINERAL WEATHERING(4,1)|MODELING BICARBONATE(4,1)|MOLTEN LAKE(4,1)|MULTISTAGE REACTOR(4,1)|NATURAL WEATHERING REACTION(4,1)|OAE STRATEGY(4,1)|OUTFLOW CONDUIT(4,1)|PARTICULATE INORGANIC CARBON(4,1)|PLANNED ENHANCED WEATHERING PROJECT(4,1)|PLURAL REFERENT(4,1)|POWDERED LIMESTONE(4,1)|PREDICTION MODEL(4,1)|PRETREATMENT MODEL(4,1)|PROLONGED RESIDENCE(4,1)|REACTANT TRANSPORT MODEL(4,1)|RIVER BASIN INTEREST(4,1)|RIVER GRADIENT(4,1)|SCOTCH BROAD REGION(4,1)|SHALLOW GRADIENT(4,1)|SPECIES POPULATION(4,1)|STOICHIOMETRIC CARBONATE(4,1)|SUCCESSIVE MONITORING STATION(4,1)|SUSTAINED ENVIRONMENTAL HAZARD(4,1)|TARGET BASIN PH(4,1)|TRANSPORTATION NETWORK(4,1)|UNSTATED FEATURE(4,1)|WASTE MATERIAL(4,1)|WEATHERING RATE ITERATIVE MEASUREMENT(4,1)|TARGET RANGE(3,10)|CARBONATION WEATHERING(3,6)|CARBONIC ACID(3,5)|CLAY(3,4)|ROAD NETWORK(3,4)|TARGET VALUE(3,4)|ALKALI METAL(3,2)|CACO(3,2)|CONTAMINANT(3,2)|FARMLAND(3,2)|FLOW VELOCITY(3,2)|GROUNDWATER(3,2)|INLAND WATER TARGET(3,2)|MITIGATE GLOBAL WARMING(3,2)|TARGET INLAND WATER EMISSION(3,2)|TARGET INLAND WATER PH(3,2)|TURBULENCE(3,2)|WATER OPENING TARGET INLAND(3,2)|WATERSHED(3,2)|WEATHERED AREA(3,2)|WEATHERING REACTION RATE(3,2)|WOODLAND(3,2)|ADJACENT HYDROLOGIC OBSERVATION STATION(3,1)|ALKALINE NEUTRAL RIVER(3,1)|ALKALINITY CONDITION(3,1)|ATTESTATION(3,1)|BASELINE CONDITION PH(3,1)|BICARBONATE CONCENTRATION DIFFERENCE(3,1)|CARBONATE SPECIES(3,1)|DISSOLUTION REACTION(3,1)|DOWNSTREAM SENSOR(3,1)|ECOLOGICALLY COMMON BENEFIT(3,1)|FUEL COMBUSTION(3,1)|GASEOUS ENVIRONMENT(3,1)|GRINDING COST MINIMIZATION(3,1)|HYDROGRAPHIC DISCHARGE RATE(3,1)|INLAND WATER ALKALINITY(3,1)|INLAND WATERWAY(3,1)|INORGANIC CARBON SPECIES SUM(3,1)|MAINTENANCE VEHICLE(3,1)|MINERAL BASED ALKALINE MODIFIER(3,1)|NONLINEAR RELATIONSHIP(3,1)|NUTRIENT(3,1)|OPERATIONAL ITEM(3,1)|PERIODIC MEASUREMENT(3,1)|PRETREATMENT PHASE(3,1)|PRETREATMENT RELATIONSHIP(3,1)|PROTON ACCEPTOR EXCESS(3,1)|REAGENT(3,1)|RIVER NATURE(3,1)|SOLUBLE INORGANIC CARBON(3,1)|SOLUBLE ORGANIC CARBON MINERALIZATION(3,1)|STABLE BICARBONATE(3,1)|STRONG ACID IMPAIRED CARBONATION(3,1)|TARGET INLAND WATER DOSING(3,1)|TOXIC IONIC ALUMINUM REDUCTION(3,1)|TURBULENT WATER ZONE(3,1)|WEATHERED REGION(3,1)|DEVIATION(2,2)|EMISSION RATE(2,2)|SOURCE LAKE(2,2)|ACCESSIBILITY(2,1)|ACID ANION(2,1)|ADJACENT BASIN(2,1)|ALKALI TREATMENT(2,1)|ALKALINE PRODUCT(2,1)|AQUEOUS PRODUCT TRANSPORTATION(2,1)|ATLANTIC OCEAN(2,1)|BASELINE DATA(2,1)|BASICITY(2,1)|BASIN DOWNSTREAM POINT(2,1)|BIODIVERSITY(2,1)|BYPRODUCT(2,1)|CALCULATED SOLUBILITY CONSTANT(2,1)|CARBON DIOXIDE FLUX(2,1)|CARBON MODEL(2,1)|CARBON MONITORING(2,1)|CARBON VARIABLE DIFFERENCE(2,1)|CARBONATE ALKALINE MODIFIER ADDITION(2,1)||(IN202417047811)|CARBON DIOXIDE REMOVAL(100,85)|CO2(100,42)|PRETREATMENT ALKALINITY STATUS(100,31)|CARBON DIOXIDE(100,29)|ATMOSPHERIC CARBON DIOXIDE(100,8)|FRESHWATER(100,4)|TARGET INLAND WATER(88,206)|CARBON VARIABLE(43,62)|NONCARBONATE ALKALINE AMENDMENT(41,1)|FRESHWATER RIVER(39,1)|ACCELERATED CARBONATION(37,1)|ECOSYSTEM COBENEFIT(35,2)|ALKALINITY INTRODUCTION(33,1)|ALKALINE MATERIAL(32,156)|ALKALINITY(29,46)|CARBON CAPTURE STRATEGY(29,26)|CONNECTIVITY(27,19)|CALCIUM RICH PLAGIOCLASE FELDSPAR(27,2)|ESTABLISHED PRETREATMENT ALKALINITY STATUS(27,2)|RIVER MOUTH(26,53)|REACTOR(25,55)|BODY WATERSHED(23,12)|INCREASED CARBONATION(23,10)|TREATMENT SITE(22,44)|SEA(21,50)|ALKALINE AMENDMENT APPLICATION INFRASTRUCTURE(21,14)|ATTRIBUTE(21,1)|ADDITION SITE(20,90)|MEAN PH(20,6)|WATERSHED BOUNDARY(20,2)|INCREASING ALKALINITY(19,11)|ECOLOGICAL VARIABLE VALUE(19,2)|METAMORPHIC ROCK RICH(19,2)|CARBON DIOXIDE DRAWDOWN(19,1)|FRESHWATER LAKE(19,1)|INLAND WATER(18,34)|BASELINE CALCULATION(18,2)|ANTHROPOGENIC IMPACT(17,4)|BICARBONATE MEASUREMENT(17,2)|ECOLOGICAL VARIABLE WATER VARIABLE(17,2)|ALKALINITY INCREASED DELIVERY(17,1)|WEATHERING(16,8)|WETLAND(16,4)|MAGNESIUM RICH PYROXENE(16,2)|ESTUARY(15,5)|CARBONATE ROCK(15,2)|RIVER(14,16)|GRAY EMISSION(14,15)|CEMENT KILN DUST(14,3)|TOXIN(14,1)|WEATHERING ZONE(13,14)|TURBULENT WATER(13,5)|CONCENTRATED CO2(13,4)|STATISTICAL RELATION(13,2)|TARGET INLAND WATER INTEREST(13,2)|TREATMENT MONITORING SITE(12,8)|CARBONATION WEATHERING REACTION(12,5)|CARBON VARIABLE MEASUREMENT(12,2)|SPECIALIZED LIMING BARGE EMERSION(12,1)|LAKE(11,9)|CRUSHED DOLOMITIC LIMESTONE(11,2)|BOAT(10,11)|PCO(10,11)|AIRPLANE(10,2)|HELICOPTER(10,2)|NEIGHBORING HYDROMETRIC STATION(10,2)|WOLLASTONITE(10,2)|INCREASING PH(10,1)|CARBONATE MINERAL(9,7)|CARBON CAPTURE CALCULATION(9,6)|CARBON VARIABLE VALUE(9,5)|EXTRA ALKALINITY(9,5)|DRY POWDER(9,4)|HEADWATER LAKE(9,4)|MICROBIAL COMMUNITY(9,3)|QUARRY(9,3)|AUTOMATED LIME DOSER(9,2)|BASALT(9,2)|BODY DISCHARGE(9,2)|DRONE(9,2)|NEUTRALIZING STRONG ACID(9,2)|OLIVINE(9,2)|PRECIPITATION(9,2)|PRETREATMENT CONNECTIVITY STATUS(9,2)|RIVER WATER(9,2)|SNOWMELT(9,2)|CARBONATION WEATHERING STOICHIOMETRY(9,1)|LARGE TARGET INLAND WATER(9,1)|AVERAGE GRAIN SIZE(8,6)|BASELINE VALUE(8,6)|WEST RIVER(8,6)|ECOLOGY(8,4)|CALCITE(8,3)|FLOOD PLAIN BOUNDARY(8,2)|FLUE GAS LINK(8,2)|FLUVIAL GEOMORPHOLOGY(8,2)|INCREASING DELIVERY(8,2)|LAKE LIMNOLOGICAL CHARACTERIZATION(8,1)|DAM(7,8)|POND(7,3)|ATLANTIC SALMON POPULATION(7,2)|CONVEYER BELT(7,2)|DRAINAGE NETWORK CONFIGURATION(7,2)|LOGISTICAL RESOURCE(7,2)|NEIGHBORING WATERSHED(7,2)|RIVER DRAINAGE NETWORK SLOPE(7,2)|SATURATION LEVEL(7,2)|TRUCK(7,2)|DOLOMITE ALKALINE AMENDMENT(7,1)|ESTIMATING CO2 DRAWDOWN(7,1)|ORGANIZATION GHG INVENTORY(7,1)|IDENTIFIED TARGET INLAND WATER(6,6)|PATHWAY(6,5)|SLURRY(6,4)|ACIDIC RIVER(6,3)|CARBONATE ANION(6,3)|CEMENT PLANT(6,3)|HCOS DELIVERY(6,3)|ALKALINE AMENDMENT MASS(6,2)|CO2 EVASION REDUCTION(6,2)|LAND ENHANCED WEATHERING PROJECT(6,2)|REYNOLD NUMBER(6,2)|SEQUESTERING CO2(6,2)|ALKALINE AMENDMENT STRATEGY(6,1)|ALKALINE MATERIAL DOSING RATE(6,1)|BICARBONATE EXPORT FLUX(6,1)|CARBONATION STOICHIOMETRY(6,1)|INDIRECT GHG EMISSION(6,1)|WATERSHED HYDROLOGY(6,1)|FIXED STATION(5,4)|STORAGE SILO(5,3)|ALKALINITY GENERATION(5,2)|BASELINE SCENARIO(5,2)|CALCIUM OXIDE(5,2)|MEAN ANNUAL DISCHARGE(5,2)|MICROBIAL CATALYST(5,2)|PROJECT ORGANIZATION(5,2)|REACTOR INTRODUCTION(5,2)|WATER ALKALINITY STATUS(5,2)|WATERSHED MODEL(5,2)|WETLAND DISTRIBUTION(5,2)|ALKALINE AMENDMENT DELIVERY(5,1)|ALKALINE AMENDMENT DOSAGE(5,1)|AMBIENT ALKALINITY DISCRETE ESTIMATE(5,1)|CARBON DIOXIDE VALUE(5,1)|FUEL COMBUSTION ONSITE(5,1)|KILLAG RIVER SITE(5,1)|MINERAL ALKALINE AMENDMENT(5,1)|PULVERIZED ALKALINE MINERAL(5,1)|ALKALINE EARTH METAL(4,4)|CONTINUOUS MONITORING PERMANENT STATION(4,4)|CO2 DISSOLUTION(4,3)|NON CARBONATE ALKALINE AMENDMENT(4,3)|ACID NEUTRALIZATION(4,2)|CACOS(4,2)|CARBON DRAWDOWN(4,2)|CARBON VARIABLE TARGET RANGE(4,2)|HEAVY METAL(4,2)|LABORATORY ANALYSIS(4,2)|TRANSITION ALKALINITY WATER(4,2)|WATER SLOPE(4,2)|ALKALINE DISSOLUTION(4,1)|ALKALINE MINERAL EXPOSURE(4,1)|AQUATIC DELIVERY CONDUIT BREAKDOWN(4,1)|AQUEOUS ENVIRONMENT SALINITY(4,1)|BASELINE CONDITION FUTURE PREDICTION(4,1)|BASELINE PROJECTION(4,1)|BIOGEOCHEMICAL MODEL(4,1)|CARBONATION WEATHERING RATE(4,1)|COARSE GRAVEL(4,1)|CUMULATIVE DAILY(4,1)|DAILY TIMESTEP(4,1)|DEPLOYING SILICATE(4,1)|DOCUMENT ECOSYSTEM(4,1)|DOLOMITE AMENDMENT(4,1)|DOSING ALGORITHM VARIABLE(4,1)|DRAINAGE NETWORK ALKALINITY STATUS(4,1)|ECOLOGICAL CONCERN(4,1)|ECOSYSTEM HEALTH(4,1)|ENTRAINMENT THRESHOLD(4,1)|ESTUARY RIVER MOUTH(4,1)|FINAL ALKALINE AMENDMENT(4,1)|FORESTED LAND(4,1)|GRANITE BEDROCK(4,1)|H2CO PROPORTION(4,1)|LAKE BASIN(4,1)|MICROBIAL AMENDMENT(4,1)|MINERAL WEATHERING(4,1)|MODEL ESTABLISHED PRETREATMENT(4,1)|MODIFIED ALKALINE AMENDMENT(4,1)|NET ECOSYSTEM PRODUCTION(4,1)|PLANNED ENHANCED WEATHERING PROJECT(4,1)|PMOL RRR2S(4,1)|POWDERED LIMESTONE(4,1)|PRECISE CARBONATION(4,1)|RESIDENCY PROLONGATION(4,1)|STRATIFICATION SCHEDULE(4,1)|SUSPENDED SEDIMENT ESTHETIC CONCERN(4,1)|TARGET WATERSHED PH(4,1)|TURNOVER REGIME(4,1)|UNDERWATER TERRAIN(4,1)|WASTE MATERIAL(4,1)|WATERSHED INTEREST(4,1)|WATERSHED REACH(4,1)|CARBONATION WEATHERING(3,7)|CARBONIC ACID(3,5)|TARGET VALUE(3,5)|BROAD REGION(3,3)|WATER DISCHARGE(3,3)|ACCESSIBILITY(3,2)|ALKALI METAL(3,2)|ALKALINE AMENDMENT ADDITION INFRASTRUCTURE(3,2)|CONTAMINANT(3,2)|DRAINAGE WATER(3,2)|FLOW VELOCITY(3,2)|GROUNDWATER(3,2)|IMPOUNDMENT(3,2)|INCREASED TURBIDITY(3,2)|INDUSTRIALLY PRODUCED ALKALINE MATERIAL(3,2)|TURBULENCE(3,2)|ALKALINE REAGENT(3,1)|ALKALINITY ADDITION ECOLOGICAL COBENEFIT(3,1)|AMENDMENT INCREASED CO2 EMISSION(3,1)|ANIONIC SPECIES(3,1)|AVERAGE CO2 FLUX(3,1)|BICARBONATE DELIVERY(3,1)|BICARBONATE FLUX(3,1)|BODY LIME DOSER(3,1)|CARBONATE SILICATE CYCLE(3,1)|CHANNEL STRAIGHTNESS(3,1)|CO2 CARBON SPECIES(3,1)|CO2 MEASUREMENT(3,1)|DISCHARGE REGIME STABILITY(3,1)|EARTH HISTORY(3,1)|ESTIMATE CO2(3,1)|ESTIMATING RIVER DISCHARGE(3,1)|FINE GRAINSIZE(3,1)|GLOBAL BIOGEOCHEMICAL CYCLE(3,1)|HCOS SHOW MEASUREMENT(3,1)|INCREASED OCEAN ALKALINITY(3,1)|INORGANIC CARBON SPECIES SUM(3,1)|LASTING ENVIRONMENTAL HARM(3,1)|MINERAL SOIL HORIZON(3,1)|NATURAL WEATHERING REACTION(3,1)|OUTFLOW CONDUIT(3,1)|PARTICULATE INORGANIC CARBON(3,1)|PRETREATMENT COLLECTION(3,1)|REACTANT GAS(3,1)|REACTANT TRANSPORT MODEL(3,1)|RELEASING CO2(3,1)|RIVER GRADIENT(3,1)|ROCK DISPERSION(3,1)|SENSING CO2(3,1)|SHALLOW GRADIENT(3,1)|SPECIES POPULATION(3,1)|STABLE DISCHARGE REGIME(3,1)|STRONG ACID IMPAIRED CARBONATION(3,1)|TARGET INLAND WATER CARBONATE(3,1)|TOOL PROTECTION(3,1)|TRANSPORTATION NETWORK(3,1)|UNSTATED FEATURE(3,1)|UPTAKE CO2(3,1)|WATER DELIVERY CONDUIT(3,1)|WEATHERING RATE ITERATIVE MEASUREMENT(3,1)|STUDY PERIOD(2,9)|CLAY(2,4)|GROSS(2,4)|OCEAN ALKALINITY ENHANCEMENT(2,4)|ROAD NETWORK(2,4)|SHOW CO2(2,3)|TCO2E(2,3)|DEVIATION(2,2)|ACCOUNTING(2,1)|ACID ANION(2,1)|ALGAL BLOOM(2,1)|ALKALI TREATMENT(2,1)|ALKALINE MATERIAL GRAINSIZE(2,1)|ALKALINE NEUTRAL RIVER(2,1)|ALKALINE PRODUCT(2,1)|ALKALINITY STATUS FUNCTION(2,1)|ANTHROPOGENIC WATER INPUT(2,1)|AUTOMATION(2,1)|BICARBONATE CONCENTRATION DIFFERENCE(2,1)|BIODIVERSITY(2,1)|BODY CHEMISTRY(2,1)|BYPRODUCT(2,1)|C02E(2,1)|CA INCREASE(2,1)|CARBON DIOXIDE FLUX(2,1)|CARBON MODEL(2,1)|CHANNEL RAINFALL(2,1)|CO2 DRAWDOWN REMOVAL(2,1)|CO2 MASS(2,1)|CO2 POTENTIAL LOSS(2,1)|CO2 REMOVAL DRAWDOWN(2,1)|DATA COLLECTED PRETREATMENT(2,1)|DISSOLUTION REACTION(2,1)|DOWNSTREAM SENSOR(2,1)|DOWNSTREAM TREATMENT SITE(2,1)|FREQUENT CYCLE(2,1)|FULL DISSOLUTION(2,1)|GASEOUS ENVIRONMENT(2,1)|GATHER INFORMATION(2,1)|GLACIAL MASS(2,1)|GLOBAL WARMING REDUCTION(2,1)|HCOS LOSS(2,1)|HYDROLOGICAL DISCHARGE RATE(2,1)|INLAND WATER ALKALINITY(2,1)|INLAND WATERWAY(2,1)|LONGTERM STORAGE(2,1)|LOWERMOST REACH(2,1)|MAINTENANCE VEHICLE(2,1)|MASS SUM(2,1)|MONITORING STATION(2,1)|NET CO2 REMOVAL(2,1)|NONLINEAR RELATION(2,1)|NUTRIENT(2,1)|OUTSIDE CARBONATION(2,1)|PERIODIC MEASUREMENT(2,1)|PRETREATMENT PHASE(2,1)|PRETREATMENT RELATION(2,1)|REDUCED OCEAN ACIDIFICATION(2,1)|REDUCTION TOXIC IONIC ALUMINUM(2,1)|RIVER MOUTH TREATMENT SITE(2,1)|RIVER NATURE(2,1)|STABLE BICARBONATE(2,1)|STOCHASTIC RELATION(2,1)|STREAM AGITATION(2,1)|TARGET ZONE(2,1)| (US20250058273)|1. A method of removing atmospheric carbon dioxide (CO2), the method comprising:| identifying a target inland waterbody having connectivity to an ocean;| selecting one or more alkaline materials to be used;| locating one or more addition sites in the target inland waterbody;| establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; and| adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody.|2. The method of claim 1, wherein the target inland waterbody is a pond, a stream, a lake, a river, a man-made channel or conduit, an estuary, or a wetland.|3. (canceled)|4. (canceled)|5. The method of claim 1, wherein the target inland waterbody comprises at least one of a temperature of about 0° C. to about 45° C., mean pH of about 6.3 to about 9.0, a Ca2+ concentration of more than about 5 mg/L, HCO3− concentration of more than about 0.6 mM, a conductivity of more than about 50 uS/cm, or any combination thereof.|6. (canceled)|7. The method of claim 1, wherein the target inland waterbody comprises a drainage network of target inland waterbody watershed, or the target inland waterbody comprises a segment of a drainage network of the target inland waterbody watershed, and the segment of the drainage network is located between headwaters and a point of interest of the target inland waterbody watershed.|8. (canceled)|9. (canceled)|10. The method of claim 1, wherein the step of identifying the target inland waterbody comprises testing at least one carbon variable and at least one water variable of the target inland waterbody, and the step of identifying the target inland waterbody comprises testing pH and bicarbonate concentrations.|11-24. (canceled)|25. The method of claim 1, wherein the step of selecting one or more alkaline materials comprises selecting one or more alkaline materials from carbonate rocks comprising minerals such as dolomite, or calcite; igneous/metamorphic rocks rich in alkaline earth metals, such as basalt, containing such minerals as wollastonite, calcium-rich plagioclase feldspar, olivine, and calcium and magnesium-rich pyroxenes; industrially-produced alkaline material, such as cement kiln dust, magnesium or calcium oxides; industrial materials containing alkali metals or alkaline earth metals; or any combination thereof; and the median grain size of the one or more alkaline materials is between about 0.06 μm to about 64 mm.|26-32. (canceled)|33. The method of claim 1, further comprising locating one or more addition sites in the target inland waterbody, and the one or more addition sites are located adjacent to, within, above or below a dam, and/or the one or more addition sites are located adjacent to, within, or near industrial infrastructure selected from a storage silo, a reactor, a mine, a quarry and a cement plant.|34-40. (canceled)|41. The method of claim 1, wherein the pre-treatment alkalinity status is determined based on at least one of alkalinity, carbon variable, strong acids and pH values of the inland waterbodies that form the drainage network from the one or more addition sites to a river mouth or combinations thereof.|42-54. (canceled)|55. The method of claim 1, wherein the one or more methods of adding the one or more alkaline materials at the one or more addition sites comprises using alkaline amendment application infrastructure, and the alkaline amendment application infrastructure is selected from a doser, a reactor, a barge, a boat, a helicopter, a truck, a conveyor belt, an airplane and a drone.|56-61. (canceled)|62. The method of claim 55, wherein the alkaline amendment application infrastructure is the reactor, and the reactor comprises a flue gas link to add concentrated CO2 to reaction that takes place in the reactor.|63. The method of claim 62, wherein the reactor is a two-staged reactor, and the reactor comprises one or more agitators.|64-66. (canceled)|67. The method of claim 1, wherein the step of adding the one or more alkaline materials further comprises establishing bicarbonate concentration at a point of interest and/or near a river mouth of the target inland waterbody watershed, and the bicarbonate concentration is established by direct measurement of one or more carbon variables, through modelling of the bicarbonate concentration, or through direct measurement of bicarbonate via sensor.|68-70. (canceled)|71. The method of claim 1, wherein the step of adding the one or more alkaline materials further comprises monitoring at one or more monitoring sites, and further comprising testing one or more of carbon variable, ecological variable, water variable and CDR values at the one or more monitoring sites to determine the response of the target inland waterbody and/or its inland waterbodies that connect the one or more addition sites of the one or more alkaline materials to a river mouth.|72-78. (canceled)|79. The method of claim 71, further comprising establishing target ranges of one or more of the carbon variable, ecological variable water variable and CDR values at the one or more monitoring sites, and further comprising adjusting the adding the one or more alkaline materials to achieve the values in the target ranges.|80. (canceled)|81. The method of claim 79, further comprising monitoring or estimating one or more of the carbon variable, ecological variable water variable and CDR values at the one or more monitoring sites.|82. The method of claim 79, further comprising calculating baseline values of the one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites.|83-91. (canceled)|92. The method of claim 1, further comprising calculating carbon capture by estimating the amount of CO2 removal from the addition of the one or more alkaline materials to the target inland waterbody, and the amount of CO2 drawdown is estimated from increased carbonation weathering, increased alkalinity, or a combination thereof.|93. (canceled)|94. The method of claim 92, wherein the estimating the amount of CO2 drawdown (CDR) is obtained from the one or more treatment sites, treatment monitoring sites, control sites, estimation of baseline values, or any combination thereof.|95. (canceled)|96. A method, comprising:| identifying a target inland waterbody having connectivity to an ocean;| selecting one or more alkaline materials to be used;| locating one or more addition sites in the target inland waterbody;| establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; and| adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody,| wherein the one or more methods of adding the one or more alkaline materials at the one or more addition sites comprises using alkaline amendment application infrastructure,| wherein the alkaline amendment application infrastructure comprises a reactor, and| wherein the reactor comprises a flue gas link to add concentrated CO2 to a reaction that takes place in the reactor.|97. A method, comprising:| identifying a target inland waterbody having connectivity to an ocean;| selecting one or more alkaline materials to be used;| locating one or more addition sites in the target inland waterbody;| establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites;| adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody; and| calculating carbon capture by estimating the amount of CO2 removal from the addition of the one or more alkaline materials to the target inland waterbody,| wherein the amount of CO2 drawdown is estimated from increased carbonation weathering, increased alkalinity, or a combination thereof, and| wherein the estimating the amount of CO2 drawdown (CDR) is obtained from the one or more treatment sites, treatment monitoring sites, control sites, estimation of baseline values, or any combination thereof. (US20250058273)|CROSS-REFERENCE TO RELATED APPLICATIONS|[0001] The application claims priority to U.S. Provisional Application No. 63/293,689 filed on Dec. 24, 2021 and U.S. Provisional Application No. 63/414,191 filed on Oct. 7, 2022, and the entire contents of each are hereby incorporated herein by reference.|(US20250058273)|FIELD|[0002] The present disclosure is directed to methods of carbon dioxide drawdown, also known as carbon dioxide removal (CDR). More specifically, the present disclosure relates to methods of CDR in inland waters, such as freshwater lakes and rivers.|BACKGROUND|[0003] The following paragraphs are not an admission that anything discussed in them is prior art or part of the knowledge of persons skilled in the art.|[0004] The carbonate silicate cycle is a global biogeochemical cycle in which the dissolved inorganic carbon (DIC) produced, primarily in the form of bicarbonate (HCO3−) and primarily from rock weathering at or below the land surface and is transferred along inland waters to oceans where it is held for storage over thousands/millions of years. This cycle is the long-term regulator of atmospheric CO2 over Earth's history (Berner and Lasaga, 1989).|[0005] In natural conditions, rock weathering occurs via reactions in soil water in the lower mineral soil horizons. Soil waters have high levels of dissolved CO2 and natural weathering reactions in soils are dominated by carbonation weathering which involve carbonic acid as a reactant.|[0006] Research on techniques for removing greenhouse gases from the atmosphere is rapidly evolving. Recent scientific reviews of the most promising and scalable CDR strategies (e.g., Fawzy et al. 2020, Terlouw et al. 2021) highlight those that employ weathering strategies such as enhanced weathering (EW) and ocean alkalinity enhancement (OAE). EW spreads large amounts of pulverized alkaline minerals onto land areas whereas OAE adds alkalinity to the ocean in coastal areas or in the open ocean (Bach et al., 2019). EW aims to increase rates of carbonation weathering of minerals and generation of alkalinity or carbonate anions, particularly bicarbonate (HCO3−), that can be transferred via rivers to long-term storage in the ocean (Hamilton et al. 2007, Fawzy et al. 2020). EW work to-date has focused on croplands (Beerling et al. 2018, 2020, Kantola et al. 2017); however, it may also be applicable to forested lands.|[0007] The application of terrestrial EW on croplands and forests is challenging due to, for example, gaining access to large swaths of land and the cost of dispersion of rock dust over vast areas. Furthermore, the reactions are relatively slow and results take time to manifest (e.g., for subaerial rock weathering and forest growth, CDR can take decades). Moreover, EW assumes that the HCO3− created during weathering is either precipitated and stored within the soil or transported from soil pore water through inland waters to the ocean for storage. However, this assumption has not been widely validated and there is evidence that some conditions may lead to a breakdown of this aquatic delivery conduit (Wallin et al. 2013, Kokic et al. 2015, Horgby et al. 2019, Bertagni and Porporato 2022).|[0008] OAE seeks to increase CDR through increasing ocean alkalinity via direct applications to the ocean surface (Renforth and Henderson, 2017, Mumma et al., 2022).|[0009] Various methods for OAE strategies have been proposed. For example, U.S. Publication No. 2012/0091066 A1 discloses a method of capturing and storing excess carbon dioxide which includes seeding melt water lakes formed on glacial masses with metal hydroxides. Patent Application No. GB 2 447 513 A describes removing carbon dioxide from the atmosphere by adding powdered limestone or dolomite to the ocean. However, the dissolution reaction associated with the strategy of direct application into ocean shows slower rates, due, for example, to higher pH in oceans (Hartmann et al., 2013). U.S. Pat. No. 6,890,497 B2 discloses a method of sequestering CO2 from a gaseous environment.|[0010] Urgent action is needed to reduce global warming to reduce the risk of severe climate change impacts, such as increased droughts, extreme rainfall events, and heatwaves (IPCC 2018, 2021). Reducing global warming depends increasingly on CDR strategies.|INTRODUCTION|[0011] The following is intended to introduce the reader to the detailed description that follows and not to define or limit the claimed subject matter.|[0012] The present disclosure provides CDR methods, which include accelerated carbonation weathering and increased alkalinity in inland waters, such as freshwater rivers, wetlands, and lakes. These methods can draw down carbon from the atmosphere while increasing inland waters' alkalinity and ability to store carbon, locking much of the carbon dioxide into more stable bicarbonate form and delivering it to the ocean for long-term storage. The methods can increase CDR, thereby contributing to the reduction of global warming.|[0013] Accordingly, the present disclosure includes methods of removing atmospheric carbon dioxide (CO2), including: identifying a target inland waterbody having connectivity to an ocean; selecting one or more alkaline materials to be used; locating one or more addition sites in the target inland waterbody; establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; and adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody.|[0014] Other features and advantages of the present disclosure will become apparent from the following detailed description. It should be understood, however, that the detailed description and the specific examples, while indicating embodiments of the application, are given byway of illustration only and the scope of the claims should not be limited by these embodiments but should be given the broadest interpretation consistent with the description as a whole.|(US20250058273)|DRAWINGS|[0015] The embodiments of the application will now be described in greater detail with reference to the drawings, in which:|[0016] FIG. 1A shows a flow chart of a method of removing atmospheric carbon dioxide according to exemplary embodiments of the application.|[0017] FIG. 1B shows a schematic view of an exemplary target inland waterbody and waterbody terms used in the method of the present application.|[0018] FIG. 1C shows a schematic view of connectivity types of the target inland waterbody to the ocean as a function of alkalinity status of the drainage network of the addition site.|[0019] FIG. 1D shows a schematic view of alkaline amendment application methods and infrastructure; top left) a doser; top right) a reactor; and bottom) a barge.|[0020] FIG. 1E shows a schematic view of the locations of monitoring sites as a function of alkalinity status.|[0021] FIG. 2 shows an exemplary watershed with two alkaline material addition sites and a control and treatment monitoring site network.|[0022] FIG. 3 shows a flowchart of an exemplary process to loop carbon variable and stream chemistry data back to refine the dosing algorithm for target inland waterbody lime dosers.|[0023] FIG. 4 shows an exemplary flowchart of a method of calculating the amount of CO2 removed from the atmosphere following the addition of the alkaline material to the target inland waterbody.|[0024] FIG. 5 shows a flowchart of an exemplary method of quantifying ecological co-benefits of the alkalinity addition.|[0025] FIG. 6 shows maps of sampling site locations in Nova Scotia, Canada in exemplary embodiments of the application. KRC is a control monitoring site, directly upstream of the alkaline addition site. KRT is a treatment monitoring site at the downstream end of the weathering zone. AF_WR is a treatment monitoring site at the river mouth.|[0026] FIG. 7 shows schematics for the design of continuous monitoring stations of A) a control site (KCR) and B) a treatment site downstream of the weathering zone (KRT) for the Killag River sites in exemplary embodiments of the application. pH, temperature, and conductivity were measured by a sonde, and CO2 concentration was measured by an eosGP.|[0027] FIG. 8. shows measurements of HCO3 concentrations versus distance at upstream control sites (7UKR, 9UWR, KRC), and at downstream treatment sites (KRT, KRB, BD_WR, X1WR, and AF_WR) in exemplary embodiments of the application (Case A Step F following the method in FIG. 1A). HCO3 concentrations are derived from field measurements of CO2 concentration and pH and the program CO2SYS (Lewis and Wallace, 1998). Sites are as situated in FIG. 6.|[0028] FIG. 9 shows locations of a 2021 survey of short (30 min) carbon dioxide flux and pH measurements in the broader region of Nova Scotia. These measurements identify high CO2 evasion flux levels and can be used to determine the potential for the method of the present application in new target inland waterbodies. Average CO2 flux is shown for each site in μmol m−2s−1.|[0029] FIG. 10 shows CO2 flux for continuous monitoring permanent stations from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site at the bottom of a weathering zone and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site at the bottom of a weathering zone.|[0030] FIG. 11 shows a relationship between CO2 flux and pH at continuous monitoring permanent stations from Jun. to Dec. 1, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site.|[0031] FIG. 12 shows a relationship between CO2 flux and water temperature at continuous monitoring permanent stations from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site.|[0032] FIG. 13 shows CO2 concentration for continuous monitoring permanent stations from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site.|[0033] FIG. 14 shows a relationship between CO2 concentration and pH at monitoring stations from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site.|[0034] FIG. 15 shows a relationship between CO2 concentration and water temperature at stations in exemplary embodiments of the application from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River: WRC=control site; WRT=treatment site.|[0035] FIG. 16 shows CO2 flux at locations in the broader region of Nova Scotia of A) sites with longer-term deployments (over 12 hours) and of B) sites with shorter term deployments (over 30 minutes).|[0036] FIG. 17 shows a relationship between CO2 flux and pH at all spot check locations in the broader region of Nova Scotia. These measurements identify high CO2 evasion flux levels and can be used to determine the potential for the method of the present application in new target inland waterbodies.|[0037] FIG. 18A shows the CDR calculation for Case A, for the initial alkaline amendment application method (following Step F in FIG. 1A). Here the CDR is CDR_gross, not including grey emissions.|[0038] FIG. 18B shows the CDR calculation for Case A, for the modified alkaline amendment application method (following Step H in FIG. 1A). Here the CDR is CDR_gross, not including grey emissions.|[0039] FIG. 18C shows the CDR calculation for Case B, for the initial and final alkaline amendment application method (following Step F in FIG. 1A). Here the CDR is CDR_gross, not including grey emissions.|[0040] FIG. 19 shows a schematic view of carbon removal mechanisms for the CDR of the method of the present application.|[0041] FIG. 20 shows and example of types of models used to generate baseline scenario values for Case B. FIG. 20A shows the model established between the control and treatment sites based on data collected pre-treatment.|[0042] FIG. 20B shows the projection of baseline values based on post-treatment control data using the model established in the pre-treatment stage.|(US20250058273)|DESCRIPTION OF VARIOUS EMBODIMENTS|[0043] Various apparatuses or methods will be described below to provide an example of an embodiment of each claimed invention. No embodiment described below limits any claimed invention and any claimed invention may cover apparatuses and methods that differ from those described below. The claimed inventions are not limited to apparatuses and methods having all of the features of any one apparatus or method described below, or to features common to multiple or all of the apparatuses or methods described below. It is possible that an apparatus or method described below is not an embodiment of any claimed invention. Any invention disclosed in an apparatus or method described below that is not claimed in this document may be the subject matter of another protective instrument, for example, a continuing patent application, and the applicant(s), inventor(s) and/or owner(s) do not intend to abandon, disclaim or dedicate to the public any such invention by its disclosure in this document.|Definitions|[0044] Unless otherwise indicated, the definitions and embodiments described in this and other sections are intended to be applicable to all embodiments and aspects of the present disclosure herein described for which they are suitable as would be understood by a person skilled in the art.|[0045] In understanding the scope of the present disclosure, the term “comprising” and its derivatives, as used herein, are intended to be open ended terms that specify the presence of the stated features, elements, components, groups, integers, and/or steps, but do not exclude the presence of other unstated features, elements, components, groups, integers and/or steps. The foregoing also applies to words having similar meanings such as the terms, “including”, “having” and their derivatives.|[0046] Terms of degree such as “substantially”, “about” and “approximately” as used herein mean a reasonable amount of deviation of the modified term such that the end result is not significantly changed. These terms of degree should be construed as including a deviation of at least ±10% of the modified term if this deviation would not negate the meaning of the word it modifies.|[0047] As used in this disclosure, the singular forms “a”, “an” and “the” include plural references unless the content clearly dictates otherwise.|[0048] The term “alkalinity” as used herein refers to the buffering capacity of water. More specifically, alkalinity is the excess of proton acceptors (bases) in a solution (Middelburg et al., 2020). It is a measure of the ability of the water body to neutralize acids and bases and thus maintain a stable pH level.|[0049] The term “carbon dioxide removal” (CDR) as used herein refers to is a process in which carbon dioxide gas (CO2) is removed from the atmosphere and sequestered (for example for long period of time), resulting in net CO2 removal from the atmosphere. CDR may refer to the strategies used to achieve CDR for example to reduce climate change impacts, and to the amounts of CO2 that has been removed from the atmosphere and delivered to long-term storage in the ocean.|[0050] The term “carbonation weathering” as used herein refers to the weathering reactions in which H2CO3* is a reactant and which result in carbon drawdown and generation of alkalinity or carbonate anions, for example HCO3−, as a product.|[0051] The term “CO2 drawdown” or “CO2 removal” or CDR as used herein refers to a process that removes CO2 from the atmosphere. The CO2 drawdown/removal can include short term or long-term storage. CDR_gross refers to carbon dioxide removal amounts that does not consider grey emissions (G). CDR_net refers to carbon dioxide removal amounts from which grey emissions are subtracted (i.e., CDR_gross−G=CDR_net).|[0052] The term “carbonic acid” as used herein comprises the two carbon species of CO2(aq) and H2CO3, due to the fast reaction kinetics of CO2 in water, and is represented herein as H2CO3*.|[0053] The term “strong acid” as used herein comprises acids that have a pKa value less than that of carbonic acid. The pKa of strong acids is most often less than −1.74, and includes but is not limited to sulphuric acid, nitric acid, hydrochloric acid, and organic acids such as those found in dissolved organic carbon.|[0054] The term “enhanced weathering” (EW) as used herein refers to a process that increases carbonation weathering rates through, for example, the addition of alkaline materials to land, freshwaters or oceans, and/or exposure of alkaline minerals to chemical/microbial conditions that increase carbonation weathering rates.|[0055] The term “dissolved inorganic carbon” (DIC) as used herein refers to the sum of the inorganic carbon species and is comprised of compounds such as carbon dioxide (CO2), carbonic acid (H2CO3), bicarbonate (HCO3−) and carbonate (CO32−).|[0056] The term “organic carbon” (OC) as used herein refers to organic compounds in water, either in dissolved or particulate form. Dissolved organic carbon (DOC) is operationally defined as OC that passes through a small mesh (e.g., 0.22 to 0.7 um).|[0057] The term “pCO2” as used herein refers to the partial pressure of CO2 in a fluid (i.e., in a gas or liquid).|[0058] The term “target inland waterbody” as used herein refers to an inland waterbody that is selected for removing atmospheric carbon dioxide (CO2) according to the method of the present application.|[0059] The term “inland waters” as used herein refers to the hydrologic flow pathways comprising surface waters, ponds, streams, rivers, wetlands, lakes and estuaries that connect the land surface to the oceans.|[0060] The term “inland waterbody” is a segment of inland waters.|[0061] The term “doser” as used herein refers to a structure that both stores and disperses materials into environments, including watersheds and inland waters.|[0062] The term “bathymetric data” as used herein refers to information about the depths, volumes and shapes of underwater terrain, which may include stratification and turnover regimes.|[0063] The term “limnological characterizations” as used herein refers to aspects of the biological, chemical, physical, and geological characteristics and functions of inland waters, including discharge rate.|[0064] The term “stratification” as used herein refers to a change in the temperature at different depths in a body of water and is due to the change in water's density with gradients in temperature and salinity.|[0065] The term “discharge rate” as used herein refers to the quantity of a fluid passing through a cross-sectional area per unit time. Discharge rate can be expressed as volume per time, e.g., m3s−1, and as length per time, e.g., m yr−1.|[0066] The term “connectivity to an ocean” as used herein means that water from the target watershed or target inland waterbody eventually drains or flows into an ocean (directly or indirectly connected to an ocean).|[0067] The term “headwater” as used herein refers to smaller water courses at higher elevations in a watershed, as opposed to the downstream larger water courses at lower elevations in the watershed.|[0068] The term “background condition” as used herein refers to conditions that are projected to occur at treatment sites had the treatment not taken place.|[0069] The term “monitoring site” as used herein refers to a location along an inland waterway where data are collected to quantify values of carbon variables, water variables and/or ecological variables.|[0070] The term “treatment site” as used herein refers to a monitoring site downstream of the alkaline addition location.|[0071] The term “control site” as used herein refers to a monitoring site not affected by the treatment, for example, upstream of the addition site, or in neighbouring watersheds.|[0072] The term “dosing algorithm” as used herein refers to a formula or method that specifies the amount of alkaline material to be added to the target inland waterbody per unit of time.|[0073] The term “addition site” as used herein refers to a location where alkaline material is added to an inland waterbody.|[0074] The term “carbon variables” as used herein refers to the variables that represent amounts and flows of inorganic carbon in inland waters and the chemical states that determine the amounts and flows, which include alkalinity, DIC, particulate inorganic carbon, HCO3− (bicarbonate), H2CO3 (carbonic acid), H2CO3*, CO32− (carbonate), dissolved CO2, pCO2, ionic strength, the carbonate system, temperature, pH, salinity and pressure.|[0075] The term “water variables” as used herein refers to the variables that represent the water quality and flows in inland waters and the chemical states that determine the amounts and flows, which include DOC, particulate organic carbon, anions, cations, metals, isotopes, microbial composition and diversity, eDNA, river discharge, Reynolds number, turbidity, conductivity, specific conductivity, dissolved oxygen, and river velocity.|[0076] The term “ecological variables” as used herein refers to the variables that represent the health of ecosystems and may refer to species population and productivity, indicators of stress in organisms, presence of invasive species or toxic microbial/algal blooms, nutrient concentrations, heavy metal and toxic substance concentrations, or biodiversity.|[0077] The term “watershed” as used herein refers to an area of land that channels rainfall and snowmelt through groundwater and inland waters that eventually flow to a defined point of interest. The watershed for a defined point of interest is the area of land that drains water to the point of interest.|[0078] The term “drainage network” as used herein refers to all inland waters that drain towards the point of interest of a watershed.|[0079] The term “river mouth” as used herein refers to a section of a river in it lowermost reach just above where it enters the ocean or a large alkaline lake. In cases where it enters the ocean, the “river mouth” may include the zone that extends through the tidal zone to the estuary.|[0080] The term “alkaline material” as used herein refers to a type of substance that when dissolved produces a pH higher than 6.0.|[0081] The term “point of interest” as used herein refers to the most downstream point of a watershed.|[0082] The term “grey emissions” as used herein refers to CO2 emissions created from the creation and delivery of the alkaline amendment to the addition site, and to CO2 emissions created during the alkaline amendment addition process.|Methods of the Present Disclosure|[0083] The present disclosure includes methods of removing atmospheric carbon dioxide (CO2) from the atmosphere (FIG. 1A), including:| - identifying a target inland waterbody having connectivity to an ocean; selecting one or more alkaline materials to be used;| - locating one or more addition sites in the target inland waterbody;| - establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; and| - adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody.|[0088] In some embodiments, the identified target inland waterbody is directly or indirectly connected to an ocean. In some embodiments, the identified target inland waterbody is directly connected to an ocean. In some embodiments, the identified target inland waterbody is indirectly connected to an ocean. In some embodiments, the target inland waterbody is a pond, a stream, a lake, a river, a man-made channel or conduit, an estuary, or a wetland. In some embodiments, the target inland waterbody is a river.|[0089] In some embodiments, the step of identifying the target inland waterbody (Step A in FIG. 1A) includes gathering information on the target inland waterbody watershed properties. In some embodiments, the step of identifying the target inland waterbody includes gathering information on at least one of hydrology, flow pathways, flow velocity, discharge rate, watershed boundaries, at least one carbon variable, at least one water variable, and at least one ecological variable of the target inland waterbody. In some embodiments, the step of identifying the target inland waterbody includes gathering information on at least one carbon variable of the target inland waterbody. In some embodiments, the step of identifying the target inland waterbody includes gathering information on at least one ecological variable of the target inland waterbody. In some embodiments, the step of identifying the target inland waterbody includes gathering information on at least one ecological variable of the target inland waterbody and/or of the ocean.|[0090] In some embodiments, other factors that are taken into consideration when identifying a target inland waterbody include, but are not limited to, accessibility along the drainage network, favorable water chemistry for carbonation weathering reactions, organic carbon concentrations, fluvial geomorphology, discharge rates and/or stability of discharge regime.|[0091] In some embodiments, the identified target inland waterbody has accessibility to vehicles, and/or boats along some or part of the drainage network along the drainage network. In some embodiments, the identified target inland waterbody has hydrological discharge rate and coefficient of variation suitable for the addition of alkalinity. In some embodiments, the identified target inland waterbody has favorable water chemistry for carbonation weathering reactions.|[0092] In some embodiments, the target inland waterbody comprises at least one of dissolved organic carbon (DOC) concentration of less than about 30 mg/L, a discharge rate of greater than about 1 m3/s or a stable discharge regime, mean pH of about 4 to about 10, water temperature of about 0° C. to about 45° C., pCO2 of above about 200 ppm, HCO3 concentration below 6 mM or more than about 0.6 mM, Ca2+ concentration of less than about 100 mg/L or more than 5 mg/L, Mg2+ concentration of less than about 40 mg/L, conductivity of about less than about 1000 uS/cm, CaCO3 concentration of less than about 1000 mg/L, specific conductivity of more than 50 uS/cm, suspended sediment concentration of less than about 1000 mg/L, a suspended sediment concentration of more than 1000 mg/L, dissolved oxygen of about 1 mg/L to about 50 mg/L, or any combination thereof.|[0093] In some embodiments, the target inland waterbody comprises a DOC concentration of about 10 mg/L to about 30 mg/L, a temperature of about 0° C. to about 45° C., mean pH of about 4.5 to about 6.3 or about 6.3 to about 9.0, a pCO2 of above about 1000 ppm; a Ca2+ concentration of less than about 10 mg/L or more than about 5 mg/L, a Mg2+ concentration of less than about 5 mg/L, a specific conductivity of less than about 50 uS/cm or more than 50 uS/cm, a CaCO3 concentration of less than about 10 mg/L, HCO3− concentration of about 0 to about 1 mM or more than about 0.6 mM, a suspended sediment concentration of less than about 50 mg/L, or greater than 50 mg/L, a dissolved oxygen of about 7 mg/L to about 20 mg/L, or any combination thereof.|[0094] In some embodiments, the target inland waterbody comprises at least one of a temperature of about 0° C. to about 45° C., mean pH of about 6.3 to about 9.0, a Ca2+ concentration of more than about 5 mg/L, HCO3− concentration of more than about 0.6 mM, a conductivity of more than about 50 uS/cm, or any combination thereof.|[0095] In some embodiments, the target inland waterbody comprises at least one of Reynold's number of greater than about 2300, discharge rate of greater than about 1 m3/s, or temperature of less than about 45° C.|[0096] In some embodiments, other factors that are taken into consideration when identifying a target inland waterbody include, but are not limited to, social context, distance to sources of the alkaline material, presence of other carbon dioxide removal or enhanced weathering projects in the watershed, presence of anthropogenic point source inputs to the target inland waterbody, importance and/or title for indigenous peoples, and transportation network.|[0097] In some embodiments, the target inland waterbody is identified based on at least one of a distance to sources of the one or more alkaline materials, a distance to industrial infrastructure, a distance to logistical resources and presence of an existing land-based enhanced weathering project. In some embodiments, the industrial infrastructure includes, but is not limited to, flue gas sources or a dam. In some embodiments, the target inland waterbody is identified based on, at least one of, to minimize the distance to sources of the one or more alkaline materials, to minimize the distance to industrial infrastructure, to minimize the distance to logistical resources and availability to connect to the existing or future land-based enhanced weathering projects.|[0098] In some embodiments, the target inland waterbody includes the entire drainage network (a drainage network) of the target inland waterbody watershed. In some embodiments, the target inland waterbody includes a segment of the drainage network of the target inland waterbody watershed (FIG. 1B). In some embodiments, the segment of the drainage network is located between headwaters and a point of interest of the target inland waterbody watershed. The size of the segment of the drainage network can be varied and is within the consideration of the person skilled in the art.|[0099] In some embodiments, the step of identifying the target inland waterbody includes testing at least one carbon variable and at least one water variable in the target inland waterbody. In some embodiments, the step of identifying the target inland waterbody includes testing pH and bicarbonate concentration. In some embodiments, the step of identifying the target inland waterbody includes testing pH and at least one of pCO2 or CO2 concentration.|[0100] In some embodiments, the step of identifying the target inland waterbody includes testing at least two carbon variables and at least one water variable in the target inland waterbody. In some embodiments one of the two carbon variables is pH. In some embodiments, one of the two carbon variables is bicarbonate concentration. In some embodiments, a first carbon variable of the at least two carbon variables is pH and a second carbon variable is pCO2. In some embodiments, the first carbon variable is pH and the second carbon variable is CO2 concentration.|[0101] In some embodiments, the target inland waterbody is acidic, with a mean pH of less than about 7.0, prior to adding the alkaline material. In some embodiments, the target inland waterbody is acidic, with a mean pH of less than about 6, prior to adding the alkaline material.|[0102] In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material. In some embodiments, the target inland waterbody is not acidic with a mean pH of above about 6.3, prior to adding the alkaline material. In some embodiments, the target inland waterbody is not acidic with a mean pH of above about 7.0, prior to adding the alkaline material. In some embodiments, the mean pH is determined by taking the average of one or more annual, bi-annual, monthly, weekly, daily, hourly, or continuous measurements of the pH.|[0103] In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material. In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material, with bicarbonate concentrations of the target inland waterbody at the river mouth below carbonate saturation concentrations. In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material, with the bicarbonate concentrations at the river mouth of the target inland waterbody between 0 and about 6000 μmol/L.|[0104] In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material based on the measurements of the mean pH, alkalinity, and/or at least one carbon variable. In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material, with bicarbonate concentrations of the target inland waterbody at the river mouth are below saturation level or between 0 and about 6000 μmol/L and the mean pH is below about 7.0 or is above about 7.0, or the mean pH is above about 6.0 or above about 6.3.|[0105] In some embodiments, the step of selecting one or more alkaline materials (Step B in FIG. 1A) includes selecting one or more alkaline materials from: carbonate rocks comprising minerals such as dolomite, or calcite; igneous/metamorphic rocks rich in alkaline earth metals, such as basalt, containing such minerals as wollastonite, calcium-rich plagioclase feldspar, olivine, and calcium and magnesium-rich pyroxenes; industrially-produced alkaline material, such as cement kiln dust, magnesium or calcium oxides; industrial materials containing alkali metals or alkaline earth metals; or any combination thereof. In some embodiments, the alkaline material is crushed dolomite.|[0106] In some embodiments, the alkaline material to be used is selected based on at least one of the following characteristics/considerations: the proximity to the source of the one or more alkaline materials, local availability, the cost of the one or more alkaline materials, an opportunity to reuse waste materials, the absence of impurities, toxins, heavy metals or other undesirable attributes, the ability to provide ecosystem co-benefits, such as the addition of calcium and magnesium in inland waters deficient in these elements, ability to optimize the introduction of alkalinity and increased pH when dissolved in freshwater, ability to optimize the speed of reaction within acceptable environmental limits. Considering local availability, the type of alkaline material is also chosen based on the following: to introduce of alkalinity and increase pH when dissolved in freshwater; to maintain a fast speed of reaction within acceptable environmental limits; to have full dissolution to avoid increased turbidity; and to optimize ecological co-benefits, such as via the introduction of base cations such as calcium. In cases where strong acids are present in the target inland waterbody, use of carbonate-based alkaline amendments needs to be carefully monitored to check for CO2 losses due to strong acid weathering and/or low pH. An example of a method to address the potential loss of CO2 from the application of carbonate minerals to inland waters with higher levels of strong acids is to 1) pre-treat the water so that the strong acids have been removed before the addition of carbonate minerals, either upstream or in a one- or two-stage reactor, or 2) add the carbonate minerals in a reactor where the CO2 produced from strong acid weathering with the carbonate minerals is not released to the atmosphere, and/or rediverted into weathering of new carbonate minerals.|[0107] Method to safely deploy silicate minerals and other materials that may produce clays during dissolution or carbonation weathering, e.g., deploying silicates in impoundments or lakes where clays can settle out, so that increased turbidity downstream is prevented; an example of a method to address this is through the introduction of a reactor step to the process, where the clays settle out before the treated water is introduced into the inland waterbody.|[0108] Method to safely deploy alkaline materials, such as silicate minerals and cement kiln dust (CKD) that may release toxic metals during dissolution or carbonation weathering, e.g., adding the alkaline materials first in a reactor, where the alkaline material is dissolved in a reactor and contaminants are removed through microbial or chemical processes, until the contaminants are reduced to acceptable levels in the treated water when it is ready to be dispersed into the inland waterbody.|[0109] In some embodiments, chemical properties, weathering reactions, physics and/or kinetics of the one or more alkaline materials to be used in the target inland waterbody are determined using any methods known to the person skilled in the art.|[0110] In some embodiments, a median grain size of the one or more alkaline materials is between about 0.02 μm to about 120 mm. In some embodiments, the median grain size of the one or more alkaline materials is between about 0.03 μm to about 100 mm. In some embodiments, the median grain size of the one or more alkaline materials is between about 0.05 μm to about 80 mm. In some embodiments, the median grain size of the one or more alkaline materials is between about 0.06 μm (clay) to about 64 mm (coarse gravel).|[0111] In some embodiments, the method further includes adding microbial communities to the one or more alkaline materials, a reactor, or directly to the target inland waterbody. In some embodiments, the addition of the microbial communities to the one or more alkaline materials, a reactor, or the target inland waterbody promotes and accelerates carbonation weathering reactions (Uroz et al., 2009).|[0112] In some embodiments, the method further comprises adjusting the composition and grainsize of the one or more alkaline materials. In some embodiments, the composition of the one or more alkaline materials is adjusted via the addition of substances prior to distribution or by sourcing alternative one or more alkaline materials. In some embodiments, the grainsize of alkaline materials is adjusted in response to iterative measurements of weathering rates where the smaller grain size is used to increase weathering rates. In some embodiments, the grainsize is optimized for weathering vs the need to grind to finer grainsizes, based on individual site conditions. In some embodiments, said adjustments and optimizations avoid the deposition of the one or more alkaline materials at the bottom of the target inland waterbody and keep sediment entrained until the weathering reaction is complete, while minimizing the costs of grinding. Sediment deposition and entrainment thresholds are site-specific, and are a function of one of the following: water velocity, friction (bed material grain size), straightness of channel/fluvial geomorphology, and/or channel slope (and thus stream power/shear stress conditions in the mixing zone).|[0113] In some embodiments, the locating one or more addition sites in the target inland waterbody includes testing target inland waterbody. In some embodiments, testing target inland waterbody includes testing at least one of water slope, water discharge, anthropogenic impacts, drainage network configuration, bedrock type, ecology, species at risk or any combination thereof.|[0114] In some embodiments, the method further includes locating one addition site in the target inland waterbody. In some embodiments, the method includes locating two or more addition sites in the target inland waterbody. In some embodiments, two addition sites are located in the target inland waterbody. The selected number of addition sites is based on the size of the segment of the target inland waterbody, the waterbody's watershed properties, hydrology, pathways, flow, discharge, carbon variables, water variables, ecological variables and the like.|[0115] In some embodiments, the one or more addition sites are located adjacent to a dam. In some embodiments, the one or more addition sites are located within a dam. In some embodiments, the one or more addition sites are located above a dam. In some embodiments, the one or more addition sites are located below a dam.|[0116] In some embodiments, the one or more addition sites are located adjacent to an industrial infrastructure. In some embodiments, the one or more addition sites are located within an industrial infrastructure. In some embodiments, the one or more addition sites are located near an industrial infrastructure. In some embodiments, the industrial infrastructure is a storage silo or a reactor. In some embodiments, the industrial infrastructure is a mine, a quarry or a cement plant. As such, in some embodiments, industrial infrastructure is selected from a storage silo, a reactor, a mine, a quarry and a cement plant. In some embodiments, the industrial infrastructure produces CO2 as a byproduct or a waste product.|[0117] In some embodiments, the one or more addition sites have turbulent waters immediately downstream of the one or more addition sites. In this embodiment, the speed and efficiency of the method of the present disclosure is increased due to physical agitation and chemical disequilibrium induced by turbulent stream flow.|[0118] In some embodiments, the one or more addition sites are located in the headwaters of the target inland waterbody. In some embodiments, the one or more addition sites are located above the river mouth of the target inland waterbody.|[0119] In some embodiments, the pre-treatment alkalinity status (Step C in FIG. 1A) is established at the one or more addition sites. In some embodiments, the pre-treatment alkalinity status is established at the one or more monitoring sites. In some embodiments, the pre-treatment alkalinity status (Step C in FIG. 1A) at the one or more addition sites in the target inland waterbody is obtained by direct measurement of the target inland waterbody using any method known in the art. In some embodiments, the pre-treatment alkalinity status is obtained by modelling of the target inland waterbody using any method known in the art. In some embodiments, the pre-treatment alkalinity status is obtained by direct measurement of the target inland waterbody and modelling of the target inland waterbody. In some embodiments, the pre-treatment alkalinity status is obtained from an existing land-based enhanced weathering project. In some embodiments, the pre-treatment alkalinity status is obtained from a separate monitoring program or project.|[0120] In some embodiments, the pre-treatment alkalinity status is determined based on at least one of alkalinity, carbon variable, strong acids and pH values of the inland waterbodies that form the drainage network from the one or more addition sites to the estuary river mouth or combinations thereof.|[0121] In some embodiments, the pre-treatment alkalinity status at the one or more addition sites and/or monitoring sites in the target inland waterbody is low alkalinity, transition alkalinity or high alkalinity. In some embodiments, the pre-treatment alkalinity status at the one or more addition sites and/or monitoring sites in the target inland waterbody is low alkalinity. In some embodiments, the pre-treatment alkalinity status at the one or more addition and/or monitoring sites is transition alkalinity. In some embodiments, the pre-treatment alkalinity status at the one or more addition sites and/or monitoring sites in the target inland waterbody is high alkalinity.|[0122] In some embodiments, the one or more addition sites and/or monitoring sites in the target inland waterbody have low pH. In some embodiments, the one or more addition sites and/or monitoring sites in the target inland waterbody have high pH. In some embodiments, the one or more addition sites and/or monitoring sites in the target inland waterbody have low concentration of strong acids. In some embodiments, the one or more addition sites in the target inland waterbody have high concentration of strong acids.|[0123] In some embodiments, the pre-treatment alkalinity status (Step C in FIG. 1A) at the one or more addition sites and/or monitoring sites in the target inland waterbody is established after the step of selecting one or more alkaline materials (Step B in FIG. 1A). In some embodiments, the pre-treatment alkalinity status (Step C in FIG. 1A) at the one or more addition sites and/or monitoring sites in the target inland waterbody is established prior to the step of selecting one or more alkaline materials (Step B in FIG. 1A).|[0124] In some embodiments, the one or more methods of adding one or more alkaline materials are determined based on a carbon capture strategy selected from increased carbonation weathering, increased alkalinity, or a combination thereof (FIG. 19). In some embodiments, the carbon capture strategy is increased carbonation weathering. In some embodiments, the carbon capture strategy is increased alkalinity. In some embodiments, the carbon capture strategy is a combination of increased carbonation weathering and increased alkalinity. In some embodiments, the addition of the one or more alkaline materials simultaneously increases alkalinity and the carbonation weathering process in the target inland waterbody, with both processes resulting in a reduction of CO2 evasion, removal or drawdown of CO2 from the atmosphere. In some embodiments, the addition of the one or more alkaline materials simultaneously increases alkalinity and the carbonation weathering process in the target inland waterbody, with both processes resulting in a reduction of CO2 evasion, removal or drawdown of CO2 from the atmosphere and increased delivery of HCO3 to the oceans.|[0125] In some embodiments, the increased carbonation weathering increases the presence of carbonation weathering reactions to produce a net increase of carbonate anions (HCO3− or CO32−) in the target inland waterbody and its drainage waters to the ocean. In some embodiments, the carbonation weathering reaction is shown in Equation (1):|CaMg(CO3)2+H2O+CO2->Ca2++Mg2++2HCO3−  (1)|[0126] In some embodiments, the increased alkalinity increases the efficiency of the delivery of HCO3− or CO32− to the oceans, by increasing the proportion of DIC in the target inland waterbody as HCO3 and CO32− and thus reducing the proportion of H2CO3*. In some embodiments, the HCO3− or CO32− is delivered to the ocean for long term storage. In some embodiments, increased alkalinity increases the concentration of DIC in the target inland waterbody. In some embodiments, increased alkalinity increases the concentration of HCO3− in the target inland waterbody. In some embodiments, increasing the pH in the target inland waterbody above about 6.0 or above about 6.3 drives carbonate speciation away from dissolved CO2 to anionic species such as bicarbonate (HCO3−) or CO32−. In some embodiments, increased alkalinity reduces the partial pressure of CO2 in the water, reduces CO2 evasion, and therefore increases the target inland waterbody's capacity to uptake CO2, to store carbon as HCO3 or CO32− (i.e., increasing the target inland waterbody carbonate content). In some embodiments, increased alkalinity increases CO2 removal/drawdown from the atmosphere, and increases delivery of bicarbonate for long-term storage in the ocean.|[0127] In some embodiments, the carbon capture strategy is determined based on a connectivity type of the target inland waterbody to the ocean selected from connected, disconnected or partially connected to the ocean. In some embodiments, the target inland waterbody is connected to the ocean. In some embodiments, the target inland waterbody is partially connected to the ocean. In some embodiments, the target inland waterbody is disconnected from the ocean (FIG. 1C).|[0128] In some embodiments, when the connectivity type is connected, the carbon capture strategy is increased carbonation weathering.|[0129] In some embodiments, when the connectivity type is disconnected, the carbon capture strategy is increased alkalinity. In some embodiments, when the connectivity type is disconnected, the carbon capture strategy is a combination of increased alkalinity and increased carbonation weathering.|[0130] In some embodiments, when the connectivity type is partially connected, the carbon capture strategy is increased carbonation weathering. In some embodiments, when the connectivity type is partially connected, the carbon capture strategy is increased alkalinity. In some embodiments, when the connectivity type is partially connected, the carbon capture strategy is a combination of increased carbonation weathering and increased alkalinity.|[0131] In some embodiments, when the target inland waterbody is disconnected or partially connected to the ocean and there is an existing or planned enhanced weathering project in the watershed, the carbon capture strategy is increased alkalinity. In this embodiment, the increased alkalinity strategy in combination with the existing or planned enhanced weathering project in the watershed increases the efficiency of carbonate delivery to the ocean and thereby achieving long-term sequestration of a land-based enhanced weathering project.|[0132] In some embodiments, the carbon capture strategy comprises additional CDR pathways such as increasing the alkalinity of the receiving ocean, net ecosystem production, for example where acidification has caused lasting environmental harm, changing rates of dissolved organic carbon mineralization, or a combination thereof.|[0133] In some embodiments, the connectivity type of the target inland waterbody to the ocean is determined. In some embodiments, the connectivity is determined based on the established pre-treatment alkalinity status of the target inland waterbody. In some embodiments, the pre-treatment alkalinity status is determined based on at least one of alkalinity, carbon variable, strong acids and pH values of the inland waterbodies that form the drainage network from the one or more addition sites to the river mouth or combinations thereof (FIGS. 1C and 1E).|[0134] The alkalinity is a measure of the ability of the water body to neutralize acids and bases and thus maintain a stable pH level. In some embodiments, the alkalinity (Alk) is defined as in Equation (2):|Alk=(HCO3−)+2(CO3−)+(OH−)−(H+)  (2)|wherein molar concentrations are used and alkalinity has units of eq/L. In some embodiments, adding bases adds OH− to the solution, making alkalinity increase. In some embodiments, reducing rates of acid addition, and thus reducing H+ addition rates to solution, making alkalinity increase.|[0135] In some embodiments, the alkalinity status is classified as:| - low (proportion of DIC as H2CO3*>90%);| - transition (proportion of 90%>H2CO3*>10%); and| - high (proportion of DIC as H2CO3*<10%).|[0139] In some embodiments, the alkalinity status is classified as:| - low (proportion of DIC as H2CO3*>50%);| - transition (proportion of 50%>H2CO3*>5%); and| - high (proportion of DIC as H2CO3*<5%).|[0143] In some embodiments, the alkalinity status is classified as:| - low (proportion of DIC as H2CO3*>30%);| - transition (proportion of DIC as H2CO3* being less than 30% but greater than >10%); and| - high (proportion of DIC as H2CO3*<10%).|[0147] The proportion of DIC as H2CO3* is dependent in part on the temperature and salinity of its aqueous environment. In some embodiments, the proportion H2CO3* is derived from equations set forth in Chapter 9 of Mook et al. 2000, the entire contents of which are hereby incorporated herein by reference.|[0148] In some embodiments, the one or more methods of adding alkaline material comprising adding the alkaline material directly into a waterbody.|[0149] In some embodiments, the one or more methods of adding the one or more alkaline materials at the one or more addition sites (Step E in FIG. 1A) comprise using alkaline amendment application infrastructure (for example as in FIG. 1D). The alkaline amendment application infrastructure which can be used in the method of the present disclosure includes any type of infrastructure for delivering the alkaline amendment (the one or more alkaline materials) into the target inland waterbody. Examples of infrastructure include but are not limited to a doser, a reactor, a barge, a boat, a helicopter, a truck, a conveyor belt, an airplane and a drone (FIG. 1D). In some embodiments, the alkaline amendment application infrastructure is selected from a doser, a reactor, a barge and a boat.|[0150] In some embodiments, the alkaline amendment application infrastructure is the doser. In some embodiments, the doser automatically or semi-automatically delivers the one or more alkaline materials directly into a waterbody. In some embodiments, the doser delivers the one or more alkaline materials on a continuous, frequent or periodic cycle. In some embodiments, the doser delivers the one or more alkaline materials to the target inland waterbody as a dry powder or as a slurry (the alkaline material is mixed with water). In some embodiments, the doser delivers the one or more alkaline materials to the target inland waterbody having the mean pH of above 6.0. In some embodiments, the doser delivers the one or more alkaline materials to the target inland waterbody having the mean pH of above 7.0. In some embodiments, the doser delivers the one or more alkaline materials to the target inland waterbody having the mean pH of above 6.3.|[0151] In some embodiments, the doser is located such that turbulent waters are immediately downstream of the addition site to increase rates of weathering reactions and maximize dissolution.|[0152] In some embodiments, the dosing rate of the one or more alkaline materials is between about 0.14 to about 16 mg per L of river water.|[0153] In some embodiments, the one or more alkaline materials are added using the doser together with adding the one or more alkaline materials directly to the one or more addition sites in the same target inland waterbody watershed.|[0154] In some embodiments, the alkaline amendment application infrastructure is the reactor. In some embodiments, the alkaline amendment application infrastructure is an open reactor. In some embodiments, the alkaline amendment application infrastructure is a closed reactor. The reactor which can be used in the method of the present disclosure includes any type of enclosed or open volume or structure in which a chemical reaction takes place. Examples of reactors include, but are not limited to, structures for separate storage of reactant(s), structures for delivery of gaseous reactants (e.g., flue gas), structures for delivery of aqueous products or reaction medium into the reactor (e.g., water from river), outflow conduit(s) that disperse materials from the reactor into environments, including land surfaces and waterbodies. In some embodiments, the reactor is a single-stage reactor (one volume where chemical reactions take place), a two-stage reactor (two volumes where chemical reactions take place in two stages), a multiple-stage reactor (multiple volumes where chemical reactions take place in multiple), or any combination thereof.|[0155] In some embodiments, the reactor can be used when the pH of the target inland waterbody is below about 4.5, when the pH of the target waterbody is between about 4.5 to 6.3, when the pH of the target inland waterbody is above about 6.3, when strong acids are in the target inland waterbody in sufficient concentration to disrupt the carbonation weathering process, or when the pCO2 in the target inland waterbody is low. In some embodiments, the reactor can be used when the addition site is too close to the ocean for the complete dissolution of the alkaline material to occur before entry to the ocean or larger waterbody. In some embodiments, the reactor is used when the alkaline material settles in the target inland waterbody before dissolution occurs. In some embodiments, the reactor is used when the turbulence or flow in the target inland waterbody is low. In some embodiments, the reactor can be used when quantification of change in carbon variables is not possible downstream due to high levels of dilution (large target inland waterbody), or high background levels of the carbon variables exist in the receiving waters such that a change due to the addition is difficult to detect. In some embodiments, the reactor is used when there is an aesthetic concern of suspended sediment downstream of the addition site.|[0156] In some embodiments, the reactor is a two-staged reactor. In some embodiments, the two-staged reactor can be used when the one or more alkaline materials have chemical constituents, metals or impurities that require removal before being released to the target inland waterbody, when strong acids are present in the target inland waterbody in a concentration that would reduce carbonation weathering efficiency below an acceptable level, or any combination of the above.|[0157] In some embodiments, the reactor includes a flue gas link to add concentrated CO2 to a reaction that takes place in the reactor.|[0158] In some embodiments, the reactor comprises one or more agitators to speed the chemical reaction in the reactor using any agitators known in the art.|[0159] In some embodiments, the alkaline amendment application infrastructure is a barge or a boat. In some embodiments, any other floating structure which temporarily stores one or more alkaline materials can be used for the one or more methods of adding the one or more alkaline materials. In some embodiments, the barge or the boat disperses the one or more alkaline materials directly into the target inland waterbody. In some embodiments, the one or more alkaline materials are dispersed from the barge or the boat into high volume waters, slowly moving waters with a shallow gradient such as in a lake, a headwater lake, or a river, or any combination thereof. In some embodiments, the barge or boat disperses the one or more alkaline materials in the target inland waterbody as a dry powder or as a slurry (the alkaline material is mixed with water).|[0160] In some embodiments, the addition of the one or more alkaline materials to the target inland waterbodies includes, but is not limited to, spreading the one or more alkaline materials upon ice, direct addition to a flowing waterbody or its sediments, the use of rotating drums for instream agitation and mixing the one or more alkaline materials, or engineered side channels that redirect water and induce prolonged residency and dissolution.|[0161] In some embodiments, the alkaline amendment application infrastructure comprises a range of storage methods, storage capacities, mixing techniques, timing, frequency and rates of delivery.|[0162] In some embodiments, carbonation weathering reactions occur in the target inland waterbody. In some embodiments, carbonation weathering reactions occur in the reactor. In some embodiments, carbonation weathering reactions occur in the target inland waterbody and in the reactor (FIG. 1D). In some embodiments, when the carbonation weathering reactions occur in the target inland waterbody, the majority of the reactions occur in the target inland waterbody. In some embodiments, when the carbonation weathering reactions occur in the reactor, the majority of the reactions occur in the reactor.|[0163] In some embodiments, the carbonation weathering reactions occur in the target inland waterbody when the barge, the boat, or the doser is used to directly add the one or more alkaline materials to the inland waterbody or when the residence time of water in contact with the one or more alkaline materials is short before being discharged to the receiving inland water body. In some embodiments, the residence time of water in contact with the alkaline material is more than about 20 minutes, less than about 20 minutes, less than about 15 minutes, or less than about 10 minutes.|[0164] In some embodiments, the carbonation weathering reactions occur in the reactor when the pH of the target inland waterbody is below about 4.5, the pH of the target inland waterbody is above about 6.3 or above about 6.5, when strong acids are present in the target inland waterbody in concentrations high enough to disrupt carbonation weathering, when pCO2 concentration of the target inland waterbody is low, when the carbonation weathering reactions are slow, when the alkaline amendment includes sulphides, when the addition site is too close to the ocean for complete dissolution to occur, when the alkaline material settles in the target inland waterbody before dissolution occurs, when the turbulence or flow of the target inland waterbody is slow, when a precise carbonation weathering efficiency rate is required, when there is an aesthetic or ecological concern with increased suspended sediment in the weathering zone downstream of the addition site, or any combination thereof.|[0165] In some embodiments, the alkaline amendment addition infrastructure is configured to have a short mean residence time for the one or more alkaline materials when it is in contact with the other reactants and water in the reactor before it is released to the waterbody, such that most of the weathering reactions take place in the inland waterbody. In some embodiments, the alkaline amendment addition infrastructure is configured to have a longer mean residence time for the one or more alkaline materials when it is in contact with the other reactants in the reactor, such that most of the weathering reactions take place in the reactor, or in both the reactor and in the inland waterbody. In some embodiments, reactors have a longer mean residence time relative to dosers, barges, boats and other forms of direct application.|[0166] In some embodiments, reactors are used to increase the speed and efficiency of the carbonation weathering reactions through manipulation of at least one of the pCO2, pH, pressure, temperature, ionic strength, concentration of strong acids, or by using more reactive alkaline materials in isolation or combination with less reactive alkaline materials.|[0167] In some embodiments, concentrated CO2 is added to the reactor. In some embodiments, the source of the concentrated CO2 for the carbonation weathering reaction is from an external source (flue gas, or gas emanating from breakdown of organic matter, or from groundwater).|[0168] In some embodiments, the source of the CO2 in the carbonation weathering reaction is from H2CO3* contained in the target inland waterbody or from CO2 contained in the atmosphere.|[0169] In some embodiments, the step of adding the one or more alkaline materials further includes establishing bicarbonate concentration at a point of interest and/or near the river mouth of the target inland waterbody watershed (FIG. 1B). In some embodiments, the bicarbonate concentration is established through direct measurement of one or more carbon variables, through modelling of the bicarbonate concentration, or through direct measurement of bicarbonate via a sensor.|[0170] In some embodiments, the one or more alkaline materials are added to the one or more addition sites at a frequency ranging from continuous frequency (e.g., every 1 minute or less) to bi-annual (approximately every two years). In some embodiments, the continuous frequency is every 3 minutes, every 5 minutes, every 10 minutes, values in between and the like. In some embodiments, the frequency of adding the one or more alkaline materials is monthly, every 3 months, once a year values in between and the like. It is to be understood that the frequency of the addition of the one or more alkaline materials is within the consideration of the person skilled in the art and any frequency is encompassed within the scope of the present disclosure.|[0171] In some embodiments, the one or more alkaline materials are added to the target inland waterbody as a dry powder. In some embodiments, the one or more alkaline materials are added to the target inland waterbody as a slurry (the alkaline material is mixed with water).|[0172] In some embodiments, the step of adding the one or more alkaline materials further includes monitoring at one or more monitoring sites (e.g., FIG. 1E and FIG. 2). In some embodiments, the one or more monitoring sites include one or more treatment sites and one or more control sites, the latter of which are sites not affected by the alkaline treatment that are used to infer the background condition of the treatment sites (FIG. 2). In some embodiments, the background conditions are conditions that are projected to occur at treatment sites had the treatment not taken place. Examples of monitoring site and background conditions include values of water variables, carbon variables or ecological variables.|[0173] In some embodiments, the one or more monitoring sites include one treatment site, two treatment sites, three treatment sites or more. In some embodiments, the one or more monitoring sites include one control site, two control sites, three control sites or more.|[0174] In some embodiments, the one or more treatment sites are located downstream of the one or more addition sites. The treatment sites can be located for example, below the weathering zone, at the river mouth, at the outflow of the one or more addition sites and between the one or more addition sites.|[0175] In some embodiments, the one or more control sites are located upstream of the one or more addition sites.|[0176] In some embodiments, the method of the present application further includes testing one or more of carbon variable, ecological variable and water variable values at the one or more monitoring sites to determine the response of the target inland waterbody and/or its inland waterbodies that connect the one or more addition sites of the one or more alkaline materials to the river mouth.|[0177] In some embodiments, the method of the present application further includes establishing target ranges of one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites. The target range is a range of values of one or more of the water variables, ecological variables and/or carbon variables that are chosen to reduce at least one of the risk of environmental harm, increase environmental co-benefits, optimize CDR, optimize cost-benefit outcomes, or any combination thereof.|[0178] In some embodiments, the method of the present application further includes monitoring or estimating the one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites.|[0179] In some embodiments, the method of the present application further includes calculating baseline values of the one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites.|[0180] In some embodiments, the one or more of the CDR, carbon variable, ecological variable and water variable values at the one or more monitoring sites are compared with the target ranges of said one or more of the carbon variable, ecological variable and water variable values. In some embodiments, when the one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites are not within the target value of said one or more of the carbon variable, ecological variable and water variable values, the one or more alkaline material addition methods are adjusted to achieve values within the target range. In some embodiments, the method of the present application further includes monitoring or estimating CDR, pCO2, pH, water temperature, salinity, discharge and HCO3−.|[0181] In some embodiments, when CDR value is not within the target value, the alkaline material addition method is adjusted to achieve CDR values within the target range. Adjustments may include having the weathering take place in a reactor where pCO2 levels are elevated, using microbial catalysts for carbonation weathering, increasing the dose of alkaline amendment, and changing the type of alkaline amendment.|[0182] In some embodiments, the method of adding the one or more alkaline materials is adjusted by adding a non-carbonate based alkaline amendment, neutralizing strong acids, or increasing the alkalinity in the drainage waters leading from the addition sites to the river mouth.|[0183] In some embodiments, in cases where carbonate minerals comprise the alkaline amendment, because of the presence of strong acids and/or low pH the alkaline amendment strategy must be adjusted so that strong acid weathering reactions do not cause a release CO2 from carbonate minerals. As an example, CO2 is produced as in Equation (3), where the reactant is calcite (CaCO3) and the acid anion is from a strong acid (HNO3−).|CaCO3+2HNO3−<->Ca2++2NO3−+H2O+CO2  (3)|[0184] In some embodiments, the carbon variable monitored or indirectly estimated at the one or more monitoring sites is bicarbonate concentration.|[0185] In some embodiments, the CDR values are calculated as in FIG. 4, and as follows:|CDR_net=C−I−G  (4)|where| - CDR_net is the carbon dioxide removed by the project (in t CO2e/Δt)| - C is increase in HCO3− delivery to ocean (in t CO2e/Δt)| - I is amount of carbon added in alkaline amendment (in t CO2e/Δt)| - G is carbon expended in grey emissions (in t CO2e/Δt)| - Δt is period of interest, can range from minutes to months to years| - CO2e is the equivalent mass of carbon dioxide|and where|C=(HCO3−t−HCO3−b)(Q)  (5)|where| - C is the increase in HCO3 delivery to the ocean at the river mouth (in t CO2e/dt)| - HCO3−t is concentration at river mouth during treatment (in t CO2e/volume)| - HCO3−b is concentration at river mouth for baseline scenario (in t CO2e/volume)| - Q is river discharge (in volume/dt)| - dt is timestep of calculation, typically ranging from minutes to weeks| - CO2e is the equivalent mass of carbon dioxide|[0198] The term “grey emissions” as used herein refers to all CO2 emissions that occur from the project and which must be removed from the estimated CDR total. Grey emissions include those emissions described by the US EPA GHG Inventory Development Process and Guidance document (https://www.epa.gov/climateleadership/ghg-inventory-development-process-and-guidance). Scope 1 emissions are direct greenhouse (GHG) emissions that occur from sources controlled by the project organization (e.g., fuel combustion onsite, maintenance vehicles, etc.). Scope 2 emissions are indirect GHG emissions associated with the purchase of energy such as electricity that is required to operate a project. Scope 2 emissions physically occur at the facility where they are generated but they are accounted for in an organization's GHG inventory because they are a result of the organization's energy use. Scope 3 emissions are the result of activities from assets not owned or controlled by the project organization and not covered by scope 1 or scope 2, sometimes referred to as value chain emissions, examples include fuel, waste and energy needs required to manufacture and deliver components needed to operate the project.|[0199] In some embodiments, the target value for CDR is such that is greater than 0. In some embodiments the target value is to have C greater than (D+G), following the definitions above.|[0200] In some embodiments, the one or more alkaline materials are added to the one or more addition sites prior to developing carbon capture strategy and/or addition method. In some embodiments, the one or more alkaline materials are added to the one or more addition sites after developing the carbon capture strategy and/or the addition method.|[0201] In some embodiments, the amount of the one or more alkaline materials is effective to enable enhanced weathering to occur and to increase the pH of the target watershed downstream of the one or more addition sites above about 5.0 is determined by the dosage and frequency of addition of the one or more alkaline materials. In some embodiments, the dosage [g_aa in Equation (6)] is about 0.1 mg/L to about 100 mg/L, less than about 1 mg/L, higher than about 100 mg/L, about 3 mg/L to about 50 mg/L, about 5 mg/L to about 30 mg/L, or about 7 mg/L to about 20 mg/L, suitably about 3 mg/L to about 15 mg/L, and is added based on site-specific data including calculated constants for solubility, discrete estimates of ambient alkalinity and real-time measurements of discharge, carbon variables, and stream pH. In some embodiments, the dosage and frequency are determined via a real-time iterative dosing method which facilitates real-time optimization and also real-time auditing of CO2 drawdown/removal to reduce the reliance on estimates of CO2 drawdown/removal via algorithms and remote sensing.|[0202] In some embodiments, the real-time iterative method comprises creation of dose/response curves for each target site for the dose and discharge and the one or more response variables. In some embodiments, the one or more response variables are selected from, but are not limited to, pH, and carbon variables. Therefore, in some embodiments, if the downstream sensor detects that one or more of the response variables are not in a target range, it would signal to a doser to increase or decrease the dose (as in FIG. 3). In some embodiments, the increase/decrease is calculated as a function of the deviation of the level from the target level, the dose/response curve, and the discharge at the time.|[0203] In some embodiments, the one or more alkaline materials are added to the one or more addition sites using a dosing algorithm. The dosing algorithm includes specific calculations and/or formulae that are used to automate the release of the one or more alkaline materials into the target inland waterbody.|[0204] A dosing algorithm is used to control the rate of alkaline addition based on one or all of continuous monitoring, modelling, periodic measurements, and a starting estimate of the concentration of alkaline product needed to achieve the desired downriver pH change, following FIG. 3 and Equation (6):|D=Q*g_aa  (6)|where| - D is dosage of alkaline amendment in mass per time, e.g., kg*s−1 | - Q is river discharge at the addition point, in volume per time, e.g., m3*s−1, obtained from field measurements or forecast from a model, or as estimated by river stage| - g_aa is concentration of alkaline amendment, in mass per volume of water (e.g., in kg*m−3), or mass per river stage|[0208] The initial value of g_aa is based on laboratory dose-response curve or an assumed concentration (e.g., 1 mg·L−1). g_aa is then adjusted after alkaline material has been added, based on values of carbon and water variables at treatment sites, including bicarbonate amounts, and/or calculated CDR values. g_aa will vary with type of alkaline material. Since g_aa is a function of both discharge and chemical properties which vary through time, chemical properties need to be monitored regularly in order to make adjustments to g_aa to achieve target levels of CDR and other carbon variables. Monitoring and adjustments can occur at a high frequency (e.g., every minute) or low frequency basis (e.g., every year), depending on the nature of the river, for example, whether the river flow and chemistry have a high coefficient of variation on a daily/monthly basis.|[0209] In some embodiments, the dosing algorithm variable Q is developed based on at least one of the water inputs to the target inland waterbody via precipitation, anthropogenic water inputs, water released from an impoundment, or snowmelt, pH, discharge or stage of the target inland waterbody. In some embodiments, the variable g_aa is based on the value of one or more carbon variables, for example, bicarbonate concentrations, or the value of one or more water variables or ecological variables. In some embodiments, the values of the variables used for the dosing algorithm are received from direct measurements, from statistical relations or models, or from process models. In some embodiments, the models may include rainfall-runoff models, hydrological models, biogeochemical models, reactive transport models, carbon models, ecological models, climate models, or any combination thereof.|[0210] In some embodiments, the values used as inputs to the dosing algorithm are obtained from one monitoring site, multiple monitoring sites, or values from continuous measuring along a drainage network extending from the addition point to the river mouth. In some embodiments, when the river mouth contains the addition site of the target inland waterbody, the river mouth comprising the addition site of the target inland waterbody.|[0211] In some embodiments, the dosing algorithm is a linear relation. In some embodiments, the dosing algorithm is a non-linear relation, for example, where g_aa is a function of Q. In some embodiments, the dosing algorithm is a stochastic relation. In some embodiments, the dosing algorithm is derived via machine-learning, deep-learning, or AI.|[0212] In some embodiments, the one or more methods of adding the one or more alkaline materials for the one or more addition sites is determined by establishing an initial alkaline material addition method for the one or more addition sites, testing the one or more treatment sites to determine if water and/or carbon variables are the within target values after one or more alkaline materials have been added and adjusting the one or more alkaline material addition methods and/or one or more alkaline materials, so that the carbon and/or water variables are within target range of said values at the one or more treatment sites. In some embodiments, one or more methods of adding the one or more alkaline materials is determined for each one of the one or more addition sites.|[0213] In some embodiments, the dosage and the frequency of application of the one or more alkaline materials addition is determined based on the volume of water being treated or discharge rates, flushing rate, temperature and stratification, water chemistry, carbon variable values, water variable values and/or particle size of the one or more alkaline materials.|[0214] In some embodiments, the dosage and frequency of addition of the one or more alkaline materials is further determined based on at least one of carbon variables, water variables, such as for example, temperature, dissolved organic carbon (DOC), HCO3− concentration or CO2 evasion rates of the water downstream of the one or more addition sites.|[0215] In some embodiments, the initial alkaline material type is selected by testing the one or more water variables and/or carbon variables at the one or more monitoring sites and by comparing values of select water and/or carbon variables to their target ranges. In some embodiments, the initial alkaline material type is selected by using a model.|[0216] In some embodiments, the method of the present application further includes calculating carbon capture by estimating the amount of CO2 drawdown/removal from the addition of the one or more alkaline materials to the target inland waterbody. In some embodiments, the carbon capture is calculated by estimating the amount of CO2 drawdown/removal from carbonation weathering processes in the target inland waterbody [Equation (7)]. In some embodiments, the carbon capture is calculated by estimating the amount of CO2 drawdown/removal from carbonation weathering processes and change in alkalinity in the target inland waterbody. The CO2 drawdown/removal is the amount of CO2 equivalent in mass per time that has been removed from the atmosphere and delivered to oceans for storage.|CDR_net=(F*E*D)−G  (7)|where| - CDR_net is the net amount of carbon removed during the project (in t CO2e/Δt)| - F is CO2 drawdown/removal during carbonation weathering of stoichiometric ratio of carbonate, calculated as the mass of CO2 drawdown/removal per mass of alkaline amendment that underwent carbonation weathering (e.g., 0.48 for dolomite) (dimensionless)| - D is the mass of alkaline amendment added (in t CO2e/Δt)| - E is carbonation weathering efficiency (1 or less) (dimensionless)| - G is carbon expended in grey emissions (in t CO2e/Δt)| - Δt is period of interest| - CO2e is the equivalent mass of carbon dioxide|[0224] In some embodiments, when carbon capture is calculated by estimating the amount of CO2 drawdown/removal from carbonation weathering processes, the mass of the one or more alkaline materials is added to the inland waterbody per unit of time, multiplied by the stoichiometry of the carbonation weathering reaction determines the amount of H2CO3*per mass of the one or more alkaline materials added [Equation (7)].|[0225] In some embodiments, when carbon capture is calculated by estimating the amount of CO2 drawdown/removal from carbonation weathering processes, when the alkalinity status of some or all of the waterbodies between the addition point and the river mouth have an alkalinity status of “low” or “transition”, the carbon capture calculations include a parameter that represents the proportion of DIC speciated as HCO3− and CO32−, as a function of one or more of pH, salinity, temperature, ionic strength and pressure.|[0226] In some embodiments, the CO2 drawdown/removal is estimated by calculating the change in carbon variable concentrations caused by the addition of alkaline amendment multiplied by the discharge at the river mouth [Equations (4) and (5)].|[0227] In some embodiments, the CO2 drawdown/removal at the river mouth is estimated by multiplying the increase in HCO3− and CO32− by the discharge at the river mouth for a period of time.|[0228] In some embodiments, the carbon capture calculations estimate CO2 drawdown/removal for a period from less than one hour to over multiple years.|[0229] In some embodiments, the carbon capture calculations are based on observations. In some embodiments, the carbon capture calculations are based on modelling, AI, deep learning, or machine learning.|[0230] In some embodiments, estimating CO2 drawdown includes testing the target inland waterbody, its drainage waters and inland waterbodies in neighboring watersheds at one or more monitoring sites.|[0231] In some embodiments, the carbon drawdown accounted for is only that in the carbonation weathering equation or the increased capacity of the inland waters to hold CO2, but not accounting for both mechanisms.|[0232] In some embodiments, the one or more monitoring sites comprising one or more treatment sites, control sites, or any combination thereof (FIG. 2).|[0233] In some embodiments, when the inland waterbodies connecting the addition site with the river mouth contain one or more low or transition alkalinity sections, the treatment sites are located at downstream end of a low or transition alkalinity waterbody segment. In some embodiments, the treatment sites are located at the bottom of the weathering zone and at the river mouth. In some embodiments, the treatment monitoring sites are located at the river mouth (FIG. 1E).|[0234] In some embodiments, when the waterbody is a transition or high alkalinity waterbody, the treatment sites are located at downstream end of weathering zone (FIG. 1E). In some embodiments, the treatment sites are located at the river mouth (FIG. 1E). In some embodiments, the treatment sites are located as shown in FIG. 1E: a) for conditions where the carbon capture strategy is to have part of all of the carbonation weathering reactions occurring in the target inland waterbody, and for conditions where the alkalinity status is low or transition; b) for conditions where the carbon capture strategy is to have part of all of the carbonation weathering reactions occurring in the target inland waterbody, and for conditions where a low or transition alkalinity waterbody flows into a transition or high alkalinity waterbody; c) for conditions where the carbon capture strategy is to have most of the carbonation weathering reactions occurring in a reactor and for conditions where the alkalinity status of the waterbodies connecting the addition site with the target inland waterbody mouth are transition or high alkalinity, and d) for conditions where the carbon capture strategy is to have most of the carbonation weathering reactions occurring in the target inland waterbody and for where the alkalinity status of the waters connecting the addition site and the target inland waterbody mouth is transition or high.|[0235] In some embodiments, the treatment site is located at the outflow of the reactor. Examples of locating the treatment site at the outflow of the reactor include estuaries with high alkalinity, weathering reactions taking place inside a reactor, with high target inland waterbody discharge such that it is difficult to detect a change in concentration of carbon variables, or in other cases where it is difficult to detect a change in concentration of carbon variables.|[0236] In some embodiments, the baseline conditions are estimated in the inland waters connecting the addition site with the river mouth. In some embodiments, the baseline conditions are estimated using modelling. In some embodiments, the baseline conditions are estimated using direct observations, or a combination of direct observations and modelling.|[0237] In some embodiments, when the weathering reactions occur in the reactor, the baseline conditions are established from the target inland waterbody chemistry directly upstream of the reactor, or inflow to reactor if using water from the target inland waterbody for the reaction.|[0238] In some embodiments, when the weathering reactions occur in the target inland waterbody, the control sites and treatment sites are tested to establish pre-treatment values for one or more of the carbon variables, ecological variables and water variables, the pre-treatment data from the control sites and the treatment sites are tested and the models/relationship between treatment and control sites are established to enable future prediction of baseline conditions at treatment sites.|[0239] In some embodiments, the change in the carbon variables at the monitoring site(s) is calculated by comparing the difference between the treatment vs baseline values of carbon variables or by multiplying the difference in the carbon variables by the target inland waterbody discharge, for timesteps ranging from one minute to multiple years [as in the example in Equation (5)].|[0240] In some embodiments, the ecological variables are measured to quantify additional ecosystem co-benefits (FIG. 5).|[0241] The following examples of the present disclosure are intended to be illustrative but non-limiting: (US20250058273)|CROSS-REFERENCE TO RELATED APPLICATIONS|[0001] The application claims priority to U.S. Provisional Application No. 63/293,689 filed on Dec. 24, 2021 and U.S. Provisional Application No. 63/414,191 filed on Oct. 7, 2022, and the entire contents of each are hereby incorporated herein by reference.|(US20250058273)|FIELD|[0002] The present disclosure is directed to methods of carbon dioxide drawdown, also known as carbon dioxide removal (CDR). More specifically, the present disclosure relates to methods of CDR in inland waters, such as freshwater lakes and rivers.|BACKGROUND|[0003] The following paragraphs are not an admission that anything discussed in them is prior art or part of the knowledge of persons skilled in the art.|[0004] The carbonate silicate cycle is a global biogeochemical cycle in which the dissolved inorganic carbon (DIC) produced, primarily in the form of bicarbonate (HCO3−) and primarily from rock weathering at or below the land surface and is transferred along inland waters to oceans where it is held for storage over thousands/millions of years. This cycle is the long-term regulator of atmospheric CO2 over Earth's history (Berner and Lasaga, 1989).|[0005] In natural conditions, rock weathering occurs via reactions in soil water in the lower mineral soil horizons. Soil waters have high levels of dissolved CO2 and natural weathering reactions in soils are dominated by carbonation weathering which involve carbonic acid as a reactant.|[0006] Research on techniques for removing greenhouse gases from the atmosphere is rapidly evolving. Recent scientific reviews of the most promising and scalable CDR strategies (e.g., Fawzy et al. 2020, Terlouw et al. 2021) highlight those that employ weathering strategies such as enhanced weathering (EW) and ocean alkalinity enhancement (OAE). EW spreads large amounts of pulverized alkaline minerals onto land areas whereas OAE adds alkalinity to the ocean in coastal areas or in the open ocean (Bach et al., 2019). EW aims to increase rates of carbonation weathering of minerals and generation of alkalinity or carbonate anions, particularly bicarbonate (HCO3−), that can be transferred via rivers to long-term storage in the ocean (Hamilton et al. 2007, Fawzy et al. 2020). EW work to-date has focused on croplands (Beerling et al. 2018, 2020, Kantola et al. 2017); however, it may also be applicable to forested lands.|[0007] The application of terrestrial EW on croplands and forests is challenging due to, for example, gaining access to large swaths of land and the cost of dispersion of rock dust over vast areas. Furthermore, the reactions are relatively slow and results take time to manifest (e.g., for subaerial rock weathering and forest growth, CDR can take decades). Moreover, EW assumes that the HCO3− created during weathering is either precipitated and stored within the soil or transported from soil pore water through inland waters to the ocean for storage. However, this assumption has not been widely validated and there is evidence that some conditions may lead to a breakdown of this aquatic delivery conduit (Wallin et al. 2013, Kokic et al. 2015, Horgby et al. 2019, Bertagni and Porporato 2022).|[0008] OAE seeks to increase CDR through increasing ocean alkalinity via direct applications to the ocean surface (Renforth and Henderson, 2017, Mumma et al., 2022).|[0009] Various methods for OAE strategies have been proposed. For example, U.S. Publication No. 2012/0091066 A1 discloses a method of capturing and storing excess carbon dioxide which includes seeding melt water lakes formed on glacial masses with metal hydroxides. Patent Application No. GB 2 447 513 A describes removing carbon dioxide from the atmosphere by adding powdered limestone or dolomite to the ocean. However, the dissolution reaction associated with the strategy of direct application into ocean shows slower rates, due, for example, to higher pH in oceans (Hartmann et al., 2013). U.S. Pat. No. 6,890,497 B2 discloses a method of sequestering CO2 from a gaseous environment.|[0010] Urgent action is needed to reduce global warming to reduce the risk of severe climate change impacts, such as increased droughts, extreme rainfall events, and heatwaves (IPCC 2018, 2021). Reducing global warming depends increasingly on CDR strategies.|INTRODUCTION|[0011] The following is intended to introduce the reader to the detailed description that follows and not to define or limit the claimed subject matter.|[0012] The present disclosure provides CDR methods, which include accelerated carbonation weathering and increased alkalinity in inland waters, such as freshwater rivers, wetlands, and lakes. These methods can draw down carbon from the atmosphere while increasing inland waters' alkalinity and ability to store carbon, locking much of the carbon dioxide into more stable bicarbonate form and delivering it to the ocean for long-term storage. The methods can increase CDR, thereby contributing to the reduction of global warming.|[0013] Accordingly, the present disclosure includes methods of removing atmospheric carbon dioxide (CO2), including: identifying a target inland waterbody having connectivity to an ocean; selecting one or more alkaline materials to be used; locating one or more addition sites in the target inland waterbody; establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; and adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody.|[0014] Other features and advantages of the present disclosure will become apparent from the following detailed description. It should be understood, however, that the detailed description and the specific examples, while indicating embodiments of the application, are given byway of illustration only and the scope of the claims should not be limited by these embodiments but should be given the broadest interpretation consistent with the description as a whole.|(US20250058273)|DRAWINGS|[0015] The embodiments of the application will now be described in greater detail with reference to the drawings, in which:|[0016] FIG. 1A shows a flow chart of a method of removing atmospheric carbon dioxide according to exemplary embodiments of the application.|[0017] FIG. 1B shows a schematic view of an exemplary target inland waterbody and waterbody terms used in the method of the present application.|[0018] FIG. 1C shows a schematic view of connectivity types of the target inland waterbody to the ocean as a function of alkalinity status of the drainage network of the addition site.|[0019] FIG. 1D shows a schematic view of alkaline amendment application methods and infrastructure; top left) a doser; top right) a reactor; and bottom) a barge.|[0020] FIG. 1E shows a schematic view of the locations of monitoring sites as a function of alkalinity status.|[0021] FIG. 2 shows an exemplary watershed with two alkaline material addition sites and a control and treatment monitoring site network.|[0022] FIG. 3 shows a flowchart of an exemplary process to loop carbon variable and stream chemistry data back to refine the dosing algorithm for target inland waterbody lime dosers.|[0023] FIG. 4 shows an exemplary flowchart of a method of calculating the amount of CO2 removed from the atmosphere following the addition of the alkaline material to the target inland waterbody.|[0024] FIG. 5 shows a flowchart of an exemplary method of quantifying ecological co-benefits of the alkalinity addition.|[0025] FIG. 6 shows maps of sampling site locations in Nova Scotia, Canada in exemplary embodiments of the application. KRC is a control monitoring site, directly upstream of the alkaline addition site. KRT is a treatment monitoring site at the downstream end of the weathering zone. AF_WR is a treatment monitoring site at the river mouth.|[0026] FIG. 7 shows schematics for the design of continuous monitoring stations of A) a control site (KCR) and B) a treatment site downstream of the weathering zone (KRT) for the Killag River sites in exemplary embodiments of the application. pH, temperature, and conductivity were measured by a sonde, and CO2 concentration was measured by an eosGP.|[0027] FIG. 8. shows measurements of HCO3 concentrations versus distance at upstream control sites (7UKR, 9UWR, KRC), and at downstream treatment sites (KRT, KRB, BD_WR, X1WR, and AF_WR) in exemplary embodiments of the application (Case A Step F following the method in FIG. 1A). HCO3 concentrations are derived from field measurements of CO2 concentration and pH and the program CO2SYS (Lewis and Wallace, 1998). Sites are as situated in FIG. 6.|[0028] FIG. 9 shows locations of a 2021 survey of short (30 min) carbon dioxide flux and pH measurements in the broader region of Nova Scotia. These measurements identify high CO2 evasion flux levels and can be used to determine the potential for the method of the present application in new target inland waterbodies. Average CO2 flux is shown for each site in μmol m−2s−1.|[0029] FIG. 10 shows CO2 flux for continuous monitoring permanent stations from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site at the bottom of a weathering zone and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site at the bottom of a weathering zone.|[0030] FIG. 11 shows a relationship between CO2 flux and pH at continuous monitoring permanent stations from Jun. to Dec. 1, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site.|[0031] FIG. 12 shows a relationship between CO2 flux and water temperature at continuous monitoring permanent stations from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site.|[0032] FIG. 13 shows CO2 concentration for continuous monitoring permanent stations from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site.|[0033] FIG. 14 shows a relationship between CO2 concentration and pH at monitoring stations from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River in exemplary embodiments of the application: WRC=control site; WRT=treatment site.|[0034] FIG. 15 shows a relationship between CO2 concentration and water temperature at stations in exemplary embodiments of the application from June to December, 2021 of A) Killag River: KRC=control site; KRT=treatment site and B) West River: WRC=control site; WRT=treatment site.|[0035] FIG. 16 shows CO2 flux at locations in the broader region of Nova Scotia of A) sites with longer-term deployments (over 12 hours) and of B) sites with shorter term deployments (over 30 minutes).|[0036] FIG. 17 shows a relationship between CO2 flux and pH at all spot check locations in the broader region of Nova Scotia. These measurements identify high CO2 evasion flux levels and can be used to determine the potential for the method of the present application in new target inland waterbodies.|[0037] FIG. 18A shows the CDR calculation for Case A, for the initial alkaline amendment application method (following Step F in FIG. 1A). Here the CDR is CDR_gross, not including grey emissions.|[0038] FIG. 18B shows the CDR calculation for Case A, for the modified alkaline amendment application method (following Step H in FIG. 1A). Here the CDR is CDR_gross, not including grey emissions.|[0039] FIG. 18C shows the CDR calculation for Case B, for the initial and final alkaline amendment application method (following Step F in FIG. 1A). Here the CDR is CDR_gross, not including grey emissions.|[0040] FIG. 19 shows a schematic view of carbon removal mechanisms for the CDR of the method of the present application.|[0041] FIG. 20 shows and example of types of models used to generate baseline scenario values for Case B. FIG. 20A shows the model established between the control and treatment sites based on data collected pre-treatment.|[0042] FIG. 20B shows the projection of baseline values based on post-treatment control data using the model established in the pre-treatment stage.|(US20250058273)|DESCRIPTION OF VARIOUS EMBODIMENTS|[0043] Various apparatuses or methods will be described below to provide an example of an embodiment of each claimed invention. No embodiment described below limits any claimed invention and any claimed invention may cover apparatuses and methods that differ from those described below. The claimed inventions are not limited to apparatuses and methods having all of the features of any one apparatus or method described below, or to features common to multiple or all of the apparatuses or methods described below. It is possible that an apparatus or method described below is not an embodiment of any claimed invention. Any invention disclosed in an apparatus or method described below that is not claimed in this document may be the subject matter of another protective instrument, for example, a continuing patent application, and the applicant(s), inventor(s) and/or owner(s) do not intend to abandon, disclaim or dedicate to the public any such invention by its disclosure in this document.|Definitions|[0044] Unless otherwise indicated, the definitions and embodiments described in this and other sections are intended to be applicable to all embodiments and aspects of the present disclosure herein described for which they are suitable as would be understood by a person skilled in the art.|[0045] In understanding the scope of the present disclosure, the term “comprising” and its derivatives, as used herein, are intended to be open ended terms that specify the presence of the stated features, elements, components, groups, integers, and/or steps, but do not exclude the presence of other unstated features, elements, components, groups, integers and/or steps. The foregoing also applies to words having similar meanings such as the terms, “including”, “having” and their derivatives.|[0046] Terms of degree such as “substantially”, “about” and “approximately” as used herein mean a reasonable amount of deviation of the modified term such that the end result is not significantly changed. These terms of degree should be construed as including a deviation of at least ±10% of the modified term if this deviation would not negate the meaning of the word it modifies.|[0047] As used in this disclosure, the singular forms “a”, “an” and “the” include plural references unless the content clearly dictates otherwise.|[0048] The term “alkalinity” as used herein refers to the buffering capacity of water. More specifically, alkalinity is the excess of proton acceptors (bases) in a solution (Middelburg et al., 2020). It is a measure of the ability of the water body to neutralize acids and bases and thus maintain a stable pH level.|[0049] The term “carbon dioxide removal” (CDR) as used herein refers to is a process in which carbon dioxide gas (CO2) is removed from the atmosphere and sequestered (for example for long period of time), resulting in net CO2 removal from the atmosphere. CDR may refer to the strategies used to achieve CDR for example to reduce climate change impacts, and to the amounts of CO2 that has been removed from the atmosphere and delivered to long-term storage in the ocean.|[0050] The term “carbonation weathering” as used herein refers to the weathering reactions in which H2CO3* is a reactant and which result in carbon drawdown and generation of alkalinity or carbonate anions, for example HCO3−, as a product.|[0051] The term “CO2 drawdown” or “CO2 removal” or CDR as used herein refers to a process that removes CO2 from the atmosphere. The CO2 drawdown/removal can include short term or long-term storage. CDR_gross refers to carbon dioxide removal amounts that does not consider grey emissions (G). CDR_net refers to carbon dioxide removal amounts from which grey emissions are subtracted (i.e., CDR_gross−G=CDR_net).|[0052] The term “carbonic acid” as used herein comprises the two carbon species of CO2(aq) and H2CO3, due to the fast reaction kinetics of CO2 in water, and is represented herein as H2CO3*.|[0053] The term “strong acid” as used herein comprises acids that have a pKa value less than that of carbonic acid. The pKa of strong acids is most often less than −1.74, and includes but is not limited to sulphuric acid, nitric acid, hydrochloric acid, and organic acids such as those found in dissolved organic carbon.|[0054] The term “enhanced weathering” (EW) as used herein refers to a process that increases carbonation weathering rates through, for example, the addition of alkaline materials to land, freshwaters or oceans, and/or exposure of alkaline minerals to chemical/microbial conditions that increase carbonation weathering rates.|[0055] The term “dissolved inorganic carbon” (DIC) as used herein refers to the sum of the inorganic carbon species and is comprised of compounds such as carbon dioxide (CO2), carbonic acid (H2CO3), bicarbonate (HCO3−) and carbonate (CO32−).|[0056] The term “organic carbon” (OC) as used herein refers to organic compounds in water, either in dissolved or particulate form. Dissolved organic carbon (DOC) is operationally defined as OC that passes through a small mesh (e.g., 0.22 to 0.7 um).|[0057] The term “pCO2” as used herein refers to the partial pressure of CO2 in a fluid (i.e., in a gas or liquid).|[0058] The term “target inland waterbody” as used herein refers to an inland waterbody that is selected for removing atmospheric carbon dioxide (CO2) according to the method of the present application.|[0059] The term “inland waters” as used herein refers to the hydrologic flow pathways comprising surface waters, ponds, streams, rivers, wetlands, lakes and estuaries that connect the land surface to the oceans.|[0060] The term “inland waterbody” is a segment of inland waters.|[0061] The term “doser” as used herein refers to a structure that both stores and disperses materials into environments, including watersheds and inland waters.|[0062] The term “bathymetric data” as used herein refers to information about the depths, volumes and shapes of underwater terrain, which may include stratification and turnover regimes.|[0063] The term “limnological characterizations” as used herein refers to aspects of the biological, chemical, physical, and geological characteristics and functions of inland waters, including discharge rate.|[0064] The term “stratification” as used herein refers to a change in the temperature at different depths in a body of water and is due to the change in water's density with gradients in temperature and salinity.|[0065] The term “discharge rate” as used herein refers to the quantity of a fluid passing through a cross-sectional area per unit time. Discharge rate can be expressed as volume per time, e.g., m3s−1, and as length per time, e.g., m yr−1.|[0066] The term “connectivity to an ocean” as used herein means that water from the target watershed or target inland waterbody eventually drains or flows into an ocean (directly or indirectly connected to an ocean).|[0067] The term “headwater” as used herein refers to smaller water courses at higher elevations in a watershed, as opposed to the downstream larger water courses at lower elevations in the watershed.|[0068] The term “background condition” as used herein refers to conditions that are projected to occur at treatment sites had the treatment not taken place.|[0069] The term “monitoring site” as used herein refers to a location along an inland waterway where data are collected to quantify values of carbon variables, water variables and/or ecological variables.|[0070] The term “treatment site” as used herein refers to a monitoring site downstream of the alkaline addition location.|[0071] The term “control site” as used herein refers to a monitoring site not affected by the treatment, for example, upstream of the addition site, or in neighbouring watersheds.|[0072] The term “dosing algorithm” as used herein refers to a formula or method that specifies the amount of alkaline material to be added to the target inland waterbody per unit of time.|[0073] The term “addition site” as used herein refers to a location where alkaline material is added to an inland waterbody.|[0074] The term “carbon variables” as used herein refers to the variables that represent amounts and flows of inorganic carbon in inland waters and the chemical states that determine the amounts and flows, which include alkalinity, DIC, particulate inorganic carbon, HCO3− (bicarbonate), H2CO3 (carbonic acid), H2CO3*, CO32− (carbonate), dissolved CO2, pCO2, ionic strength, the carbonate system, temperature, pH, salinity and pressure.|[0075] The term “water variables” as used herein refers to the variables that represent the water quality and flows in inland waters and the chemical states that determine the amounts and flows, which include DOC, particulate organic carbon, anions, cations, metals, isotopes, microbial composition and diversity, eDNA, river discharge, Reynolds number, turbidity, conductivity, specific conductivity, dissolved oxygen, and river velocity.|[0076] The term “ecological variables” as used herein refers to the variables that represent the health of ecosystems and may refer to species population and productivity, indicators of stress in organisms, presence of invasive species or toxic microbial/algal blooms, nutrient concentrations, heavy metal and toxic substance concentrations, or biodiversity.|[0077] The term “watershed” as used herein refers to an area of land that channels rainfall and snowmelt through groundwater and inland waters that eventually flow to a defined point of interest. The watershed for a defined point of interest is the area of land that drains water to the point of interest.|[0078] The term “drainage network” as used herein refers to all inland waters that drain towards the point of interest of a watershed.|[0079] The term “river mouth” as used herein refers to a section of a river in it lowermost reach just above where it enters the ocean or a large alkaline lake. In cases where it enters the ocean, the “river mouth” may include the zone that extends through the tidal zone to the estuary.|[0080] The term “alkaline material” as used herein refers to a type of substance that when dissolved produces a pH higher than 6.0.|[0081] The term “point of interest” as used herein refers to the most downstream point of a watershed.|[0082] The term “grey emissions” as used herein refers to CO2 emissions created from the creation and delivery of the alkaline amendment to the addition site, and to CO2 emissions created during the alkaline amendment addition process.|Methods of the Present Disclosure|[0083] The present disclosure includes methods of removing atmospheric carbon dioxide (CO2) from the atmosphere (FIG. 1A), including:| - identifying a target inland waterbody having connectivity to an ocean; selecting one or more alkaline materials to be used;| - locating one or more addition sites in the target inland waterbody;| - establishing pre-treatment alkalinity status at the one or more addition sites in the target inland waterbody to determine one or more methods of adding the one or more alkaline materials at the one or more addition sites; and| - adding the one or more alkaline materials to the one or more addition sites in the target inland waterbody.|[0088] In some embodiments, the identified target inland waterbody is directly or indirectly connected to an ocean. In some embodiments, the identified target inland waterbody is directly connected to an ocean. In some embodiments, the identified target inland waterbody is indirectly connected to an ocean. In some embodiments, the target inland waterbody is a pond, a stream, a lake, a river, a man-made channel or conduit, an estuary, or a wetland. In some embodiments, the target inland waterbody is a river.|[0089] In some embodiments, the step of identifying the target inland waterbody (Step A in FIG. 1A) includes gathering information on the target inland waterbody watershed properties. In some embodiments, the step of identifying the target inland waterbody includes gathering information on at least one of hydrology, flow pathways, flow velocity, discharge rate, watershed boundaries, at least one carbon variable, at least one water variable, and at least one ecological variable of the target inland waterbody. In some embodiments, the step of identifying the target inland waterbody includes gathering information on at least one carbon variable of the target inland waterbody. In some embodiments, the step of identifying the target inland waterbody includes gathering information on at least one ecological variable of the target inland waterbody. In some embodiments, the step of identifying the target inland waterbody includes gathering information on at least one ecological variable of the target inland waterbody and/or of the ocean.|[0090] In some embodiments, other factors that are taken into consideration when identifying a target inland waterbody include, but are not limited to, accessibility along the drainage network, favorable water chemistry for carbonation weathering reactions, organic carbon concentrations, fluvial geomorphology, discharge rates and/or stability of discharge regime.|[0091] In some embodiments, the identified target inland waterbody has accessibility to vehicles, and/or boats along some or part of the drainage network along the drainage network. In some embodiments, the identified target inland waterbody has hydrological discharge rate and coefficient of variation suitable for the addition of alkalinity. In some embodiments, the identified target inland waterbody has favorable water chemistry for carbonation weathering reactions.|[0092] In some embodiments, the target inland waterbody comprises at least one of dissolved organic carbon (DOC) concentration of less than about 30 mg/L, a discharge rate of greater than about 1 m3/s or a stable discharge regime, mean pH of about 4 to about 10, water temperature of about 0° C. to about 45° C., pCO2 of above about 200 ppm, HCO3 concentration below 6 mM or more than about 0.6 mM, Ca2+ concentration of less than about 100 mg/L or more than 5 mg/L, Mg2+ concentration of less than about 40 mg/L, conductivity of about less than about 1000 uS/cm, CaCO3 concentration of less than about 1000 mg/L, specific conductivity of more than 50 uS/cm, suspended sediment concentration of less than about 1000 mg/L, a suspended sediment concentration of more than 1000 mg/L, dissolved oxygen of about 1 mg/L to about 50 mg/L, or any combination thereof.|[0093] In some embodiments, the target inland waterbody comprises a DOC concentration of about 10 mg/L to about 30 mg/L, a temperature of about 0° C. to about 45° C., mean pH of about 4.5 to about 6.3 or about 6.3 to about 9.0, a pCO2 of above about 1000 ppm; a Ca2+ concentration of less than about 10 mg/L or more than about 5 mg/L, a Mg2+ concentration of less than about 5 mg/L, a specific conductivity of less than about 50 uS/cm or more than 50 uS/cm, a CaCO3 concentration of less than about 10 mg/L, HCO3− concentration of about 0 to about 1 mM or more than about 0.6 mM, a suspended sediment concentration of less than about 50 mg/L, or greater than 50 mg/L, a dissolved oxygen of about 7 mg/L to about 20 mg/L, or any combination thereof.|[0094] In some embodiments, the target inland waterbody comprises at least one of a temperature of about 0° C. to about 45° C., mean pH of about 6.3 to about 9.0, a Ca2+ concentration of more than about 5 mg/L, HCO3− concentration of more than about 0.6 mM, a conductivity of more than about 50 uS/cm, or any combination thereof.|[0095] In some embodiments, the target inland waterbody comprises at least one of Reynold's number of greater than about 2300, discharge rate of greater than about 1 m3/s, or temperature of less than about 45° C.|[0096] In some embodiments, other factors that are taken into consideration when identifying a target inland waterbody include, but are not limited to, social context, distance to sources of the alkaline material, presence of other carbon dioxide removal or enhanced weathering projects in the watershed, presence of anthropogenic point source inputs to the target inland waterbody, importance and/or title for indigenous peoples, and transportation network.|[0097] In some embodiments, the target inland waterbody is identified based on at least one of a distance to sources of the one or more alkaline materials, a distance to industrial infrastructure, a distance to logistical resources and presence of an existing land-based enhanced weathering project. In some embodiments, the industrial infrastructure includes, but is not limited to, flue gas sources or a dam. In some embodiments, the target inland waterbody is identified based on, at least one of, to minimize the distance to sources of the one or more alkaline materials, to minimize the distance to industrial infrastructure, to minimize the distance to logistical resources and availability to connect to the existing or future land-based enhanced weathering projects.|[0098] In some embodiments, the target inland waterbody includes the entire drainage network (a drainage network) of the target inland waterbody watershed. In some embodiments, the target inland waterbody includes a segment of the drainage network of the target inland waterbody watershed (FIG. 1B). In some embodiments, the segment of the drainage network is located between headwaters and a point of interest of the target inland waterbody watershed. The size of the segment of the drainage network can be varied and is within the consideration of the person skilled in the art.|[0099] In some embodiments, the step of identifying the target inland waterbody includes testing at least one carbon variable and at least one water variable in the target inland waterbody. In some embodiments, the step of identifying the target inland waterbody includes testing pH and bicarbonate concentration. In some embodiments, the step of identifying the target inland waterbody includes testing pH and at least one of pCO2 or CO2 concentration.|[0100] In some embodiments, the step of identifying the target inland waterbody includes testing at least two carbon variables and at least one water variable in the target inland waterbody. In some embodiments one of the two carbon variables is pH. In some embodiments, one of the two carbon variables is bicarbonate concentration. In some embodiments, a first carbon variable of the at least two carbon variables is pH and a second carbon variable is pCO2. In some embodiments, the first carbon variable is pH and the second carbon variable is CO2 concentration.|[0101] In some embodiments, the target inland waterbody is acidic, with a mean pH of less than about 7.0, prior to adding the alkaline material. In some embodiments, the target inland waterbody is acidic, with a mean pH of less than about 6, prior to adding the alkaline material.|[0102] In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material. In some embodiments, the target inland waterbody is not acidic with a mean pH of above about 6.3, prior to adding the alkaline material. In some embodiments, the target inland waterbody is not acidic with a mean pH of above about 7.0, prior to adding the alkaline material. In some embodiments, the mean pH is determined by taking the average of one or more annual, bi-annual, monthly, weekly, daily, hourly, or continuous measurements of the pH.|[0103] In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material. In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material, with bicarbonate concentrations of the target inland waterbody at the river mouth below carbonate saturation concentrations. In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material, with the bicarbonate concentrations at the river mouth of the target inland waterbody between 0 and about 6000 μmol/L.|[0104] In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material based on the measurements of the mean pH, alkalinity, and/or at least one carbon variable. In some embodiments, the target inland waterbody is not acidic prior to adding the alkaline material, with bicarbonate concentrations of the target inland waterbody at the river mouth are below saturation level or between 0 and about 6000 μmol/L and the mean pH is below about 7.0 or is above about 7.0, or the mean pH is above about 6.0 or above about 6.3.|[0105] In some embodiments, the step of selecting one or more alkaline materials (Step B in FIG. 1A) includes selecting one or more alkaline materials from: carbonate rocks comprising minerals such as dolomite, or calcite; igneous/metamorphic rocks rich in alkaline earth metals, such as basalt, containing such minerals as wollastonite, calcium-rich plagioclase feldspar, olivine, and calcium and magnesium-rich pyroxenes; industrially-produced alkaline material, such as cement kiln dust, magnesium or calcium oxides; industrial materials containing alkali metals or alkaline earth metals; or any combination thereof. In some embodiments, the alkaline material is crushed dolomite.|[0106] In some embodiments, the alkaline material to be used is selected based on at least one of the following characteristics/considerations: the proximity to the source of the one or more alkaline materials, local availability, the cost of the one or more alkaline materials, an opportunity to reuse waste materials, the absence of impurities, toxins, heavy metals or other undesirable attributes, the ability to provide ecosystem co-benefits, such as the addition of calcium and magnesium in inland waters deficient in these elements, ability to optimize the introduction of alkalinity and increased pH when dissolved in freshwater, ability to optimize the speed of reaction within acceptable environmental limits. Considering local availability, the type of alkaline material is also chosen based on the following: to introduce of alkalinity and increase pH when dissolved in freshwater; to maintain a fast speed of reaction within acceptable environmental limits; to have full dissolution to avoid increased turbidity; and to optimize ecological co-benefits, such as via the introduction of base cations such as calcium. In cases where strong acids are present in the target inland waterbody, use of carbonate-based alkaline amendments needs to be carefully monitored to check for CO2 losses due to strong acid weathering and/or low pH. An example of a method to address the potential loss of CO2 from the application of carbonate minerals to inland waters with higher levels of strong acids is to 1) pre-treat the water so that the strong acids have been removed before the addition of carbonate minerals, either upstream or in a one- or two-stage reactor, or 2) add the carbonate minerals in a reactor where the CO2 produced from strong acid weathering with the carbonate minerals is not released to the atmosphere, and/or rediverted into weathering of new carbonate minerals.|[0107] Method to safely deploy silicate minerals and other materials that may produce clays during dissolution or carbonation weathering, e.g., deploying silicates in impoundments or lakes where clays can settle out, so that increased turbidity downstream is prevented; an example of a method to address this is through the introduction of a reactor step to the process, where the clays settle out before the treated water is introduced into the inland waterbody.|[0108] Method to safely deploy alkaline materials, such as silicate minerals and cement kiln dust (CKD) that may release toxic metals during dissolution or carbonation weathering, e.g., adding the alkaline materials first in a reactor, where the alkaline material is dissolved in a reactor and contaminants are removed through microbial or chemical processes, until the contaminants are reduced to acceptable levels in the treated water when it is ready to be dispersed into the inland waterbody.|[0109] In some embodiments, chemical properties, weathering reactions, physics and/or kinetics of the one or more alkaline materials to be used in the target inland waterbody are determined using any methods known to the person skilled in the art.|[0110] In some embodiments, a median grain size of the one or more alkaline materials is between about 0.02 μm to about 120 mm. In some embodiments, the median grain size of the one or more alkaline materials is between about 0.03 μm to about 100 mm. In some embodiments, the median grain size of the one or more alkaline materials is between about 0.05 μm to about 80 mm. In some embodiments, the median grain size of the one or more alkaline materials is between about 0.06 μm (clay) to about 64 mm (coarse gravel).|[0111] In some embodiments, the method further includes adding microbial communities to the one or more alkaline materials, a reactor, or directly to the target inland waterbody. In some embodiments, the addition of the microbial communities to the one or more alkaline materials, a reactor, or the target inland waterbody promotes and accelerates carbonation weathering reactions (Uroz et al., 2009).|[0112] In some embodiments, the method further comprises adjusting the composition and grainsize of the one or more alkaline materials. In some embodiments, the composition of the one or more alkaline materials is adjusted via the addition of substances prior to distribution or by sourcing alternative one or more alkaline materials. In some embodiments, the grainsize of alkaline materials is adjusted in response to iterative measurements of weathering rates where the smaller grain size is used to increase weathering rates. In some embodiments, the grainsize is optimized for weathering vs the need to grind to finer grainsizes, based on individual site conditions. In some embodiments, said adjustments and optimizations avoid the deposition of the one or more alkaline materials at the bottom of the target inland waterbody and keep sediment entrained until the weathering reaction is complete, while minimizing the costs of grinding. Sediment deposition and entrainment thresholds are site-specific, and are a function of one of the following: water velocity, friction (bed material grain size), straightness of channel/fluvial geomorphology, and/or channel slope (and thus stream power/shear stress conditions in the mixing zone).|[0113] In some embodiments, the locating one or more addition sites in the target inland waterbody includes testing target inland waterbody. In some embodiments, testing target inland waterbody includes testing at least one of water slope, water discharge, anthropogenic impacts, drainage network configuration, bedrock type, ecology, species at risk or any combination thereof.|[0114] In some embodiments, the method further includes locating one addition site in the target inland waterbody. In some embodiments, the method includes locating two or more addition sites in the target inland waterbody. In some embodiments, two addition sites are located in the target inland waterbody. The selected number of addition sites is based on the size of the segment of the target inland waterbody, the waterbody's watershed properties, hydrology, pathways, flow, discharge, carbon variables, water variables, ecological variables and the like.|[0115] In some embodiments, the one or more addition sites are located adjacent to a dam. In some embodiments, the one or more addition sites are located within a dam. In some embodiments, the one or more addition sites are located above a dam. In some embodiments, the one or more addition sites are located below a dam.|[0116] In some embodiments, the one or more addition sites are located adjacent to an industrial infrastructure. In some embodiments, the one or more addition sites are located within an industrial infrastructure. In some embodiments, the one or more addition sites are located near an industrial infrastructure. In some embodiments, the industrial infrastructure is a storage silo or a reactor. In some embodiments, the industrial infrastructure is a mine, a quarry or a cement plant. As such, in some embodiments, industrial infrastructure is selected from a storage silo, a reactor, a mine, a quarry and a cement plant. In some embodiments, the industrial infrastructure produces CO2 as a byproduct or a waste product.|[0117] In some embodiments, the one or more addition sites have turbulent waters immediately downstream of the one or more addition sites. In this embodiment, the speed and efficiency of the method of the present disclosure is increased due to physical agitation and chemical disequilibrium induced by turbulent stream flow.|[0118] In some embodiments, the one or more addition sites are located in the headwaters of the target inland waterbody. In some embodiments, the one or more addition sites are located above the river mouth of the target inland waterbody.|[0119] In some embodiments, the pre-treatment alkalinity status (Step C in FIG. 1A) is established at the one or more addition sites. In some embodiments, the pre-treatment alkalinity status is established at the one or more monitoring sites. In some embodiments, the pre-treatment alkalinity status (Step C in FIG. 1A) at the one or more addition sites in the target inland waterbody is obtained by direct measurement of the target inland waterbody using any method known in the art. In some embodiments, the pre-treatment alkalinity status is obtained by modelling of the target inland waterbody using any method known in the art. In some embodiments, the pre-treatment alkalinity status is obtained by direct measurement of the target inland waterbody and modelling of the target inland waterbody. In some embodiments, the pre-treatment alkalinity status is obtained from an existing land-based enhanced weathering project. In some embodiments, the pre-treatment alkalinity status is obtained from a separate monitoring program or project.|[0120] In some embodiments, the pre-treatment alkalinity status is determined based on at least one of alkalinity, carbon variable, strong acids and pH values of the inland waterbodies that form the drainage network from the one or more addition sites to the estuary river mouth or combinations thereof.|[0121] In some embodiments, the pre-treatment alkalinity status at the one or more addition sites and/or monitoring sites in the target inland waterbody is low alkalinity, transition alkalinity or high alkalinity. In some embodiments, the pre-treatment alkalinity status at the one or more addition sites and/or monitoring sites in the target inland waterbody is low alkalinity. In some embodiments, the pre-treatment alkalinity status at the one or more addition and/or monitoring sites is transition alkalinity. In some embodiments, the pre-treatment alkalinity status at the one or more addition sites and/or monitoring sites in the target inland waterbody is high alkalinity.|[0122] In some embodiments, the one or more addition sites and/or monitoring sites in the target inland waterbody have low pH. In some embodiments, the one or more addition sites and/or monitoring sites in the target inland waterbody have high pH. In some embodiments, the one or more addition sites and/or monitoring sites in the target inland waterbody have low concentration of strong acids. In some embodiments, the one or more addition sites in the target inland waterbody have high concentration of strong acids.|[0123] In some embodiments, the pre-treatment alkalinity status (Step C in FIG. 1A) at the one or more addition sites and/or monitoring sites in the target inland waterbody is established after the step of selecting one or more alkaline materials (Step B in FIG. 1A). In some embodiments, the pre-treatment alkalinity status (Step C in FIG. 1A) at the one or more addition sites and/or monitoring sites in the target inland waterbody is established prior to the step of selecting one or more alkaline materials (Step B in FIG. 1A).|[0124] In some embodiments, the one or more methods of adding one or more alkaline materials are determined based on a carbon capture strategy selected from increased carbonation weathering, increased alkalinity, or a combination thereof (FIG. 19). In some embodiments, the carbon capture strategy is increased carbonation weathering. In some embodiments, the carbon capture strategy is increased alkalinity. In some embodiments, the carbon capture strategy is a combination of increased carbonation weathering and increased alkalinity. In some embodiments, the addition of the one or more alkaline materials simultaneously increases alkalinity and the carbonation weathering process in the target inland waterbody, with both processes resulting in a reduction of CO2 evasion, removal or drawdown of CO2 from the atmosphere. In some embodiments, the addition of the one or more alkaline materials simultaneously increases alkalinity and the carbonation weathering process in the target inland waterbody, with both processes resulting in a reduction of CO2 evasion, removal or drawdown of CO2 from the atmosphere and increased delivery of HCO3 to the oceans.|[0125] In some embodiments, the increased carbonation weathering increases the presence of carbonation weathering reactions to produce a net increase of carbonate anions (HCO3− or CO32−) in the target inland waterbody and its drainage waters to the ocean. In some embodiments, the carbonation weathering reaction is shown in Equation (1):|CaMg(CO3)2+H2O+CO2->Ca2++Mg2++2HCO3−  (1)|[0126] In some embodiments, the increased alkalinity increases the efficiency of the delivery of HCO3− or CO32− to the oceans, by increasing the proportion of DIC in the target inland waterbody as HCO3 and CO32− and thus reducing the proportion of H2CO3*. In some embodiments, the HCO3− or CO32− is delivered to the ocean for long term storage. In some embodiments, increased alkalinity increases the concentration of DIC in the target inland waterbody. In some embodiments, increased alkalinity increases the concentration of HCO3− in the target inland waterbody. In some embodiments, increasing the pH in the target inland waterbody above about 6.0 or above about 6.3 drives carbonate speciation away from dissolved CO2 to anionic species such as bicarbonate (HCO3−) or CO32−. In some embodiments, increased alkalinity reduces the partial pressure of CO2 in the water, reduces CO2 evasion, and therefore increases the target inland waterbody's capacity to uptake CO2, to store carbon as HCO3 or CO32− (i.e., increasing the target inland waterbody carbonate content). In some embodiments, increased alkalinity increases CO2 removal/drawdown from the atmosphere, and increases delivery of bicarbonate for long-term storage in the ocean.|[0127] In some embodiments, the carbon capture strategy is determined based on a connectivity type of the target inland waterbody to the ocean selected from connected, disconnected or partially connected to the ocean. In some embodiments, the target inland waterbody is connected to the ocean. In some embodiments, the target inland waterbody is partially connected to the ocean. In some embodiments, the target inland waterbody is disconnected from the ocean (FIG. 1C).|[0128] In some embodiments, when the connectivity type is connected, the carbon capture strategy is increased carbonation weathering.|[0129] In some embodiments, when the connectivity type is disconnected, the carbon capture strategy is increased alkalinity. In some embodiments, when the connectivity type is disconnected, the carbon capture strategy is a combination of increased alkalinity and increased carbonation weathering.|[0130] In some embodiments, when the connectivity type is partially connected, the carbon capture strategy is increased carbonation weathering. In some embodiments, when the connectivity type is partially connected, the carbon capture strategy is increased alkalinity. In some embodiments, when the connectivity type is partially connected, the carbon capture strategy is a combination of increased carbonation weathering and increased alkalinity.|[0131] In some embodiments, when the target inland waterbody is disconnected or partially connected to the ocean and there is an existing or planned enhanced weathering project in the watershed, the carbon capture strategy is increased alkalinity. In this embodiment, the increased alkalinity strategy in combination with the existing or planned enhanced weathering project in the watershed increases the efficiency of carbonate delivery to the ocean and thereby achieving long-term sequestration of a land-based enhanced weathering project.|[0132] In some embodiments, the carbon capture strategy comprises additional CDR pathways such as increasing the alkalinity of the receiving ocean, net ecosystem production, for example where acidification has caused lasting environmental harm, changing rates of dissolved organic carbon mineralization, or a combination thereof.|[0133] In some embodiments, the connectivity type of the target inland waterbody to the ocean is determined. In some embodiments, the connectivity is determined based on the established pre-treatment alkalinity status of the target inland waterbody. In some embodiments, the pre-treatment alkalinity status is determined based on at least one of alkalinity, carbon variable, strong acids and pH values of the inland waterbodies that form the drainage network from the one or more addition sites to the river mouth or combinations thereof (FIGS. 1C and 1E).|[0134] The alkalinity is a measure of the ability of the water body to neutralize acids and bases and thus maintain a stable pH level. In some embodiments, the alkalinity (Alk) is defined as in Equation (2):|Alk=(HCO3−)+2(CO3−)+(OH−)−(H+)  (2)|wherein molar concentrations are used and alkalinity has units of eq/L. In some embodiments, adding bases adds OH− to the solution, making alkalinity increase. In some embodiments, reducing rates of acid addition, and thus reducing H+ addition rates to solution, making alkalinity increase.|[0135] In some embodiments, the alkalinity status is classified as:| - low (proportion of DIC as H2CO3*>90%);| - transition (proportion of 90%>H2CO3*>10%); and| - high (proportion of DIC as H2CO3*<10%).|[0139] In some embodiments, the alkalinity status is classified as:| - low (proportion of DIC as H2CO3*>50%);| - transition (proportion of 50%>H2CO3*>5%); and| - high (proportion of DIC as H2CO3*<5%).|[0143] In some embodiments, the alkalinity status is classified as:| - low (proportion of DIC as H2CO3*>30%);| - transition (proportion of DIC as H2CO3* being less than 30% but greater than >10%); and| - high (proportion of DIC as H2CO3*<10%).|[0147] The proportion of DIC as H2CO3* is dependent in part on the temperature and salinity of its aqueous environment. In some embodiments, the proportion H2CO3* is derived from equations set forth in Chapter 9 of Mook et al. 2000, the entire contents of which are hereby incorporated herein by reference.|[0148] In some embodiments, the one or more methods of adding alkaline material comprising adding the alkaline material directly into a waterbody.|[0149] In some embodiments, the one or more methods of adding the one or more alkaline materials at the one or more addition sites (Step E in FIG. 1A) comprise using alkaline amendment application infrastructure (for example as in FIG. 1D). The alkaline amendment application infrastructure which can be used in the method of the present disclosure includes any type of infrastructure for delivering the alkaline amendment (the one or more alkaline materials) into the target inland waterbody. Examples of infrastructure include but are not limited to a doser, a reactor, a barge, a boat, a helicopter, a truck, a conveyor belt, an airplane and a drone (FIG. 1D). In some embodiments, the alkaline amendment application infrastructure is selected from a doser, a reactor, a barge and a boat.|[0150] In some embodiments, the alkaline amendment application infrastructure is the doser. In some embodiments, the doser automatically or semi-automatically delivers the one or more alkaline materials directly into a waterbody. In some embodiments, the doser delivers the one or more alkaline materials on a continuous, frequent or periodic cycle. In some embodiments, the doser delivers the one or more alkaline materials to the target inland waterbody as a dry powder or as a slurry (the alkaline material is mixed with water). In some embodiments, the doser delivers the one or more alkaline materials to the target inland waterbody having the mean pH of above 6.0. In some embodiments, the doser delivers the one or more alkaline materials to the target inland waterbody having the mean pH of above 7.0. In some embodiments, the doser delivers the one or more alkaline materials to the target inland waterbody having the mean pH of above 6.3.|[0151] In some embodiments, the doser is located such that turbulent waters are immediately downstream of the addition site to increase rates of weathering reactions and maximize dissolution.|[0152] In some embodiments, the dosing rate of the one or more alkaline materials is between about 0.14 to about 16 mg per L of river water.|[0153] In some embodiments, the one or more alkaline materials are added using the doser together with adding the one or more alkaline materials directly to the one or more addition sites in the same target inland waterbody watershed.|[0154] In some embodiments, the alkaline amendment application infrastructure is the reactor. In some embodiments, the alkaline amendment application infrastructure is an open reactor. In some embodiments, the alkaline amendment application infrastructure is a closed reactor. The reactor which can be used in the method of the present disclosure includes any type of enclosed or open volume or structure in which a chemical reaction takes place. Examples of reactors include, but are not limited to, structures for separate storage of reactant(s), structures for delivery of gaseous reactants (e.g., flue gas), structures for delivery of aqueous products or reaction medium into the reactor (e.g., water from river), outflow conduit(s) that disperse materials from the reactor into environments, including land surfaces and waterbodies. In some embodiments, the reactor is a single-stage reactor (one volume where chemical reactions take place), a two-stage reactor (two volumes where chemical reactions take place in two stages), a multiple-stage reactor (multiple volumes where chemical reactions take place in multiple), or any combination thereof.|[0155] In some embodiments, the reactor can be used when the pH of the target inland waterbody is below about 4.5, when the pH of the target waterbody is between about 4.5 to 6.3, when the pH of the target inland waterbody is above about 6.3, when strong acids are in the target inland waterbody in sufficient concentration to disrupt the carbonation weathering process, or when the pCO2 in the target inland waterbody is low. In some embodiments, the reactor can be used when the addition site is too close to the ocean for the complete dissolution of the alkaline material to occur before entry to the ocean or larger waterbody. In some embodiments, the reactor is used when the alkaline material settles in the target inland waterbody before dissolution occurs. In some embodiments, the reactor is used when the turbulence or flow in the target inland waterbody is low. In some embodiments, the reactor can be used when quantification of change in carbon variables is not possible downstream due to high levels of dilution (large target inland waterbody), or high background levels of the carbon variables exist in the receiving waters such that a change due to the addition is difficult to detect. In some embodiments, the reactor is used when there is an aesthetic concern of suspended sediment downstream of the addition site.|[0156] In some embodiments, the reactor is a two-staged reactor. In some embodiments, the two-staged reactor can be used when the one or more alkaline materials have chemical constituents, metals or impurities that require removal before being released to the target inland waterbody, when strong acids are present in the target inland waterbody in a concentration that would reduce carbonation weathering efficiency below an acceptable level, or any combination of the above.|[0157] In some embodiments, the reactor includes a flue gas link to add concentrated CO2 to a reaction that takes place in the reactor.|[0158] In some embodiments, the reactor comprises one or more agitators to speed the chemical reaction in the reactor using any agitators known in the art.|[0159] In some embodiments, the alkaline amendment application infrastructure is a barge or a boat. In some embodiments, any other floating structure which temporarily stores one or more alkaline materials can be used for the one or more methods of adding the one or more alkaline materials. In some embodiments, the barge or the boat disperses the one or more alkaline materials directly into the target inland waterbody. In some embodiments, the one or more alkaline materials are dispersed from the barge or the boat into high volume waters, slowly moving waters with a shallow gradient such as in a lake, a headwater lake, or a river, or any combination thereof. In some embodiments, the barge or boat disperses the one or more alkaline materials in the target inland waterbody as a dry powder or as a slurry (the alkaline material is mixed with water).|[0160] In some embodiments, the addition of the one or more alkaline materials to the target inland waterbodies includes, but is not limited to, spreading the one or more alkaline materials upon ice, direct addition to a flowing waterbody or its sediments, the use of rotating drums for instream agitation and mixing the one or more alkaline materials, or engineered side channels that redirect water and induce prolonged residency and dissolution.|[0161] In some embodiments, the alkaline amendment application infrastructure comprises a range of storage methods, storage capacities, mixing techniques, timing, frequency and rates of delivery.|[0162] In some embodiments, carbonation weathering reactions occur in the target inland waterbody. In some embodiments, carbonation weathering reactions occur in the reactor. In some embodiments, carbonation weathering reactions occur in the target inland waterbody and in the reactor (FIG. 1D). In some embodiments, when the carbonation weathering reactions occur in the target inland waterbody, the majority of the reactions occur in the target inland waterbody. In some embodiments, when the carbonation weathering reactions occur in the reactor, the majority of the reactions occur in the reactor.|[0163] In some embodiments, the carbonation weathering reactions occur in the target inland waterbody when the barge, the boat, or the doser is used to directly add the one or more alkaline materials to the inland waterbody or when the residence time of water in contact with the one or more alkaline materials is short before being discharged to the receiving inland water body. In some embodiments, the residence time of water in contact with the alkaline material is more than about 20 minutes, less than about 20 minutes, less than about 15 minutes, or less than about 10 minutes.|[0164] In some embodiments, the carbonation weathering reactions occur in the reactor when the pH of the target inland waterbody is below about 4.5, the pH of the target inland waterbody is above about 6.3 or above about 6.5, when strong acids are present in the target inland waterbody in concentrations high enough to disrupt carbonation weathering, when pCO2 concentration of the target inland waterbody is low, when the carbonation weathering reactions are slow, when the alkaline amendment includes sulphides, when the addition site is too close to the ocean for complete dissolution to occur, when the alkaline material settles in the target inland waterbody before dissolution occurs, when the turbulence or flow of the target inland waterbody is slow, when a precise carbonation weathering efficiency rate is required, when there is an aesthetic or ecological concern with increased suspended sediment in the weathering zone downstream of the addition site, or any combination thereof.|[0165] In some embodiments, the alkaline amendment addition infrastructure is configured to have a short mean residence time for the one or more alkaline materials when it is in contact with the other reactants and water in the reactor before it is released to the waterbody, such that most of the weathering reactions take place in the inland waterbody. In some embodiments, the alkaline amendment addition infrastructure is configured to have a longer mean residence time for the one or more alkaline materials when it is in contact with the other reactants in the reactor, such that most of the weathering reactions take place in the reactor, or in both the reactor and in the inland waterbody. In some embodiments, reactors have a longer mean residence time relative to dosers, barges, boats and other forms of direct application.|[0166] In some embodiments, reactors are used to increase the speed and efficiency of the carbonation weathering reactions through manipulation of at least one of the pCO2, pH, pressure, temperature, ionic strength, concentration of strong acids, or by using more reactive alkaline materials in isolation or combination with less reactive alkaline materials.|[0167] In some embodiments, concentrated CO2 is added to the reactor. In some embodiments, the source of the concentrated CO2 for the carbonation weathering reaction is from an external source (flue gas, or gas emanating from breakdown of organic matter, or from groundwater).|[0168] In some embodiments, the source of the CO2 in the carbonation weathering reaction is from H2CO3* contained in the target inland waterbody or from CO2 contained in the atmosphere.|[0169] In some embodiments, the step of adding the one or more alkaline materials further includes establishing bicarbonate concentration at a point of interest and/or near the river mouth of the target inland waterbody watershed (FIG. 1B). In some embodiments, the bicarbonate concentration is established through direct measurement of one or more carbon variables, through modelling of the bicarbonate concentration, or through direct measurement of bicarbonate via a sensor.|[0170] In some embodiments, the one or more alkaline materials are added to the one or more addition sites at a frequency ranging from continuous frequency (e.g., every 1 minute or less) to bi-annual (approximately every two years). In some embodiments, the continuous frequency is every 3 minutes, every 5 minutes, every 10 minutes, values in between and the like. In some embodiments, the frequency of adding the one or more alkaline materials is monthly, every 3 months, once a year values in between and the like. It is to be understood that the frequency of the addition of the one or more alkaline materials is within the consideration of the person skilled in the art and any frequency is encompassed within the scope of the present disclosure.|[0171] In some embodiments, the one or more alkaline materials are added to the target inland waterbody as a dry powder. In some embodiments, the one or more alkaline materials are added to the target inland waterbody as a slurry (the alkaline material is mixed with water).|[0172] In some embodiments, the step of adding the one or more alkaline materials further includes monitoring at one or more monitoring sites (e.g., FIG. 1E and FIG. 2). In some embodiments, the one or more monitoring sites include one or more treatment sites and one or more control sites, the latter of which are sites not affected by the alkaline treatment that are used to infer the background condition of the treatment sites (FIG. 2). In some embodiments, the background conditions are conditions that are projected to occur at treatment sites had the treatment not taken place. Examples of monitoring site and background conditions include values of water variables, carbon variables or ecological variables.|[0173] In some embodiments, the one or more monitoring sites include one treatment site, two treatment sites, three treatment sites or more. In some embodiments, the one or more monitoring sites include one control site, two control sites, three control sites or more.|[0174] In some embodiments, the one or more treatment sites are located downstream of the one or more addition sites. The treatment sites can be located for example, below the weathering zone, at the river mouth, at the outflow of the one or more addition sites and between the one or more addition sites.|[0175] In some embodiments, the one or more control sites are located upstream of the one or more addition sites.|[0176] In some embodiments, the method of the present application further includes testing one or more of carbon variable, ecological variable and water variable values at the one or more monitoring sites to determine the response of the target inland waterbody and/or its inland waterbodies that connect the one or more addition sites of the one or more alkaline materials to the river mouth.|[0177] In some embodiments, the method of the present application further includes establishing target ranges of one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites. The target range is a range of values of one or more of the water variables, ecological variables and/or carbon variables that are chosen to reduce at least one of the risk of environmental harm, increase environmental co-benefits, optimize CDR, optimize cost-benefit outcomes, or any combination thereof.|[0178] In some embodiments, the method of the present application further includes monitoring or estimating the one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites.|[0179] In some embodiments, the method of the present application further includes calculating baseline values of the one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites.|[0180] In some embodiments, the one or more of the CDR, carbon variable, ecological variable and water variable values at the one or more monitoring sites are compared with the target ranges of said one or more of the carbon variable, ecological variable and water variable values. In some embodiments, when the one or more of the carbon variable, ecological variable and water variable values at the one or more monitoring sites are not within the target value of said one or more of the carbon variable, ecological variable and water variable values, the one or more alkaline material addition methods are adjusted to achieve values within the target range. In some embodiments, the method of the present application further includes monitoring or estimating CDR, pCO2, pH, water temperature, salinity, discharge and HCO3−.|[0181] In some embodiments, when CDR value is not within the target value, the alkaline material addition method is adjusted to achieve CDR values within the target range. Adjustments may include having the weathering take place in a reactor where pCO2 levels are elevated, using microbial catalysts for carbonation weathering, increasing the dose of alkaline amendment, and changing the type of alkaline amendment.|[0182] In some embodiments, the method of adding the one or more alkaline materials is adjusted by adding a non-carbonate based alkaline amendment, neutralizing strong acids, or increasing the alkalinity in the drainage waters leading from the addition sites to the river mouth.|[0183] In some embodiments, in cases where carbonate minerals comprise the alkaline amendment, because of the presence of strong acids and/or low pH the alkaline amendment strategy must be adjusted so that strong acid weathering reactions do not cause a release CO2 from carbonate minerals. As an example, CO2 is produced as in Equation (3), where the reactant is calcite (CaCO3) and the acid anion is from a strong acid (HNO3−).|CaCO3+2HNO3−<->Ca2++2NO3−+H2O+CO2  (3)|[0184] In some embodiments, the carbon variable monitored or indirectly estimated at the one or more monitoring sites is bicarbonate concentration.|[0185] In some embodiments, the CDR values are calculated as in FIG. 4, and as follows:|CDR_net=C−I−G  (4)|where| - CDR_net is the carbon dioxide removed by the project (in t CO2e/Δt)| - C is increase in HCO3− delivery to ocean (in t CO2e/Δt)| - I is amount of carbon added in alkaline amendment (in t CO2e/Δt)| - G is carbon expended in grey emissions (in t CO2e/Δt)| - Δt is period of interest, can range from minutes to months to years| - CO2e is the equivalent mass of carbon dioxide|and where|C=(HCO3−t−HCO3−b)(Q)  (5)|where| - C is the increase in HCO3 delivery to the ocean at the river mouth (in t CO2e/dt)| - HCO3−t is concentration at river mouth during treatment (in t CO2e/volume)| - HCO3−b is concentration at river mouth for baseline scenario (in t CO2e/volume)| - Q is river discharge (in volume/dt)| - dt is timestep of calculation, typically ranging from minutes to weeks| - CO2e is the equivalent mass of carbon dioxide|[0198] The term “grey emissions” as used herein refers to all CO2 emissions that occur from the project and which must be removed from the estimated CDR total. Grey emissions include those emissions described by the US EPA GHG Inventory Development Process and Guidance document (https://www.epa.gov/climateleadership/ghg-inventory-development-process-and-guidance). Scope 1 emissions are direct greenhouse (GHG) emissions that occur from sources controlled by the project organization (e.g., fuel combustion onsite, maintenance vehicles, etc.). Scope 2 emissions are indirect GHG emissions associated with the purchase of energy such as electricity that is required to operate a project. Scope 2 emissions physically occur at the facility where they are generated but they are accounted for in an organization's GHG inventory because they are a result of the organization's energy use. Scope 3 emissions are the result of activities from assets not owned or controlled by the project organization and not covered by scope 1 or scope 2, sometimes referred to as value chain emissions, examples include fuel, waste and energy needs required to manufacture and deliver components needed to operate the project.|[0199] In some embodiments, the target value for CDR is such that is greater than 0. In some embodiments the target value is to have C greater than (D+G), following the definitions above.|[0200] In some embodiments, the one or more alkaline materials are added to the one or more addition sites prior to developing carbon capture strategy and/or addition method. In some embodiments, the one or more alkaline materials are added to the one or more addition sites after developing the carbon capture strategy and/or the addition method.|[0201] In some embodiments, the amount of the one or more alkaline materials is effective to enable enhanced weathering to occur and to increase the pH of the target watershed downstream of the one or more addition sites above about 5.0 is determined by the dosage and frequency of addition of the one or more alkaline materials. In some embodiments, the dosage [g_aa in Equation (6)] is about 0.1 mg/L to about 100 mg/L, less than about 1 mg/L, higher than about 100 mg/L, about 3 mg/L to about 50 mg/L, about 5 mg/L to about 30 mg/L, or about 7 mg/L to about 20 mg/L, suitably about 3 mg/L to about 15 mg/L, and is added based on site-specific data including calculated constants for solubility, discrete estimates of ambient alkalinity and real-time measurements of discharge, carbon variables, and stream pH. In some embodiments, the dosage and frequency are determined via a real-time iterative dosing method which facilitates real-time optimization and also real-time auditing of CO2 drawdown/removal to reduce the reliance on estimates of CO2 drawdown/removal via algorithms and remote sensing.|[0202] In some embodiments, the real-time iterative method comprises creation of dose/response curves for each target site for the dose and discharge and the one or more response variables. In some embodiments, the one or more response variables are selected from, but are not limited to, pH, and carbon variables. Therefore, in some embodiments, if the downstream sensor detects that one or more of the response variables are not in a target range, it would signal to a doser to increase or decrease the dose (as in FIG. 3). In some embodiments, the increase/decrease is calculated as a function of the deviation of the level from the target level, the dose/response curve, and the discharge at the time.|[0203] In some embodiments, the one or more alkaline materials are added to the one or more addition sites using a dosing algorithm. The dosing algorithm includes specific calculations and/or formulae that are used to automate the release of the one or more alkaline materials into the target inland waterbody.|[0204] A dosing algorithm is used to control the rate of alkaline addition based on one or all of continuous monitoring, modelling, periodic measurements, and a starting estimate of the concentration of alkaline product needed to achieve the desired downriver pH change, following FIG. 3 and Equation (6):|D=Q*g_aa  (6)|where| - D is dosage of alkaline amendment in mass per time, e.g., kg*s−1 | - Q is river discharge at the addition point, in volume per time, e.g., m3*s−1, obtained from field measurements or forecast from a model, or as estimated by river stage| - g_aa is concentration of alkaline amendment, in mass per volume of water (e.g., in kg*m−3), or mass per river stage|[0208] The initial value of g_aa is based on laboratory dose-response curve or an assumed concentration (e.g., 1 mg·L−1). g_aa is then adjusted after alkaline material has been added, based on values of carbon and water variables at treatment sites, including bicarbonate amounts, and/or calculated CDR values. g_aa will vary with type of alkaline material. Since g_aa is a function of both discharge and chemical properties which vary through time, chemical properties need to be monitored regularly in order to make adjustments to g_aa to achieve target levels of CDR and other carbon variables. Monitoring and adjustments can occur at a high frequency (e.g., every minute) or low frequency basis (e.g., every year), depending on the nature of the river, for example, whether the river flow and chemistry have a high coefficient of variation on a daily/monthly basis.|[0209] In some embodiments, the dosing algorithm variable Q is developed based on at least one of the water inputs to the target inland waterbody via precipitation, anthropogenic water inputs, water released from an impoundment, or snowmelt, pH, discharge or stage of the target inland waterbody. In some embodiments, the variable g_aa is based on the value of one or more carbon variables, for example, bicarbonate concentrations, or the value of one or more water variables or ecological variables. In some embodiments, the values of the variables used for the dosing algorithm are received from direct measurements, from statistical relations or models, or from process models. In some embodiments, the models may include rainfall-runoff models, hydrological models, biogeochemical models, reactive transport models, carbon models, ecological models, climate models, or any combination thereof.|[0210] In some embodiments, the values used as inputs to the dosing algorithm are obtained from one monitoring site, multiple monitoring sites, or values from continuous measuring along a drainage network extending from the addition point to the river mouth. In some embodiments, when the river mouth contains the addition site of the target inland waterbody, the river mouth comprising the addition site of the target inland waterbody.|[0211] In some embodiments, the dosing algorithm is a linear relation. In some embodiments, the dosing algorithm is a non-linear relation, for example, where g_aa is a function of Q. In some embodiments, the dosing algorithm is a stochastic relation. In some embodiments, the dosing algorithm is derived via machine-learning, deep-learning, or AI.|[0212] In some embodiments, the one or more methods of adding the one or more alkaline materials for the one or more addition sites is determined by establishing an initial alkaline material addition method for the one or more addition sites, testing the one or more treatment sites to determine if water and/or carbon variables are the within target values after one or more alkaline materials have been added and adjusting the one or more alkaline material addition methods and/or one or more alkaline materials, so that the carbon and/or water variables are within target range of said values at the one or more treatment sites. In some embodiments, one or more methods of adding the one or more alkaline materials is determined for each one of the one or more addition sites.|[0213] In some embodiments, the dosage and the frequency of application of the one or more alkaline materials addition is determined based on the volume of water being treated or discharge rates, flushing rate, temperature and stratification, water chemistry, carbon variable values, water variable values and/or particle size of the one or more alkaline materials.|[0214] In some embodiments, the dosage and frequency of addition of the one or more alkaline materials is further determined based on at least one of carbon variables, water variables, such as for example, temperature, dissolved organic carbon (DOC), HCO3− concentration or CO2 evasion rates of the water downstream of the one or more addition sites.|[0215] In some embodiments, the initial alkaline material type is selected by testing the one or more water variables and/or carbon variables at the one or more monitoring sites and by comparing values of select water and/or carbon variables to their target ranges. In some embodiments, the initial alkaline material type is selected by using a model.|[0216] In some embodiments, the method of the present application further includes calculating carbon capture by estimating the amount of CO2 drawdown/removal from the addition of the one or more alkaline materials to the target inland waterbody. In some embodiments, the carbon capture is calculated by estimating the amount of CO2 drawdown/removal from carbonation weathering processes in the target inland waterbody [Equation (7)]. In some embodiments, the carbon capture is calculated by estimating the amount of CO2 drawdown/removal from carbonation weathering processes and change in alkalinity in the target inland waterbody. The CO2 drawdown/removal is the amount of CO2 equivalent in mass per time that has been removed from the atmosphere and delivered to oceans for storage.|CDR_net=(F*E*D)−G  (7)|where| - CDR_net is the net amount of carbon removed during the project (in t CO2e/Δt)| - F is CO2 drawdown/removal during carbonation weathering of stoichiometric ratio of carbonate, calculated as the mass of CO2 drawdown/removal per mass of alkaline amendment that underwent carbonation weathering (e.g., 0.48 for dolomite) (dimensionless)| - D is the mass of alkaline amendment added (in t CO2e/Δt)| - E is carbonation weathering efficiency (1 or less) (dimensionless)| - G is carbon expended in grey emissions (in t CO2e/Δt)| - Δt is period of interest| - CO2e is the equivalent mass of carbon dioxide|[0224] In some embodiments, when carbon capture is calculated by estimating the amount of CO2 drawdown/removal from carbonation weathering processes, the mass of the one or more alkaline materials is added to the inland waterbody per unit of time, multiplied by the stoichiometry of the carbonation weathering reaction determines the amount of H2CO3*per mass of the one or more alkaline materials added [Equation (7)].|[0225] In some embodiments, when carbon capture is calculated by estimating the amount of CO2 drawdown/removal from carbonation weathering processes, when the alkalinity status of some or all of the waterbodies between the addition point and the river mouth have an alkalinity status of “low” or “transition”, the carbon capture calculations include a parameter that represents the proportion of DIC speciated as HCO3− and CO32−, as a function of one or more of pH, salinity, temperature, ionic strength and pressure.|[0226] In some embodiments, the CO2 drawdown/removal is estimated by calculating the change in carbon variable concentrations caused by the addition of alkaline amendment multiplied by the discharge at the river mouth [Equations (4) and (5)].|[0227] In some embodiments, the CO2 drawdown/removal at the river mouth is estimated by multiplying the increase in HCO3− and CO32− by the discharge at the river mouth for a period of time.|[0228] In some embodiments, the carbon capture calculations estimate CO2 drawdown/removal for a period from less than one hour to over multiple years.|[0229] In some embodiments, the carbon capture calculations are based on observations. In some embodiments, the carbon capture calculations are based on modelling, AI, deep learning, or machine learning.|[0230] In some embodiments, estimating CO2 drawdown includes testing the target inland waterbody, its drainage waters and inland waterbodies in neighboring watersheds at one or more monitoring sites.|[0231] In some embodiments, the carbon drawdown accounted for is only that in the carbonation weathering equation or the increased capacity of the inland waters to hold CO2, but not accounting for both mechanisms.|[0232] In some embodiments, the one or more monitoring sites comprising one or more treatment sites, control sites, or any combination thereof (FIG. 2).|[0233] In some embodiments, when the inland waterbodies connecting the addition site with the river mouth contain one or more low or transition alkalinity sections, the treatment sites are located at downstream end of a low or transition alkalinity waterbody segment. In some embodiments, the treatment sites are located at the bottom of the weathering zone and at the river mouth. In some embodiments, the treatment monitoring sites are located at the river mouth (FIG. 1E).|[0234] In some embodiments, when the waterbody is a transition or high alkalinity waterbody, the treatment sites are located at downstream end of weathering zone (FIG. 1E). In some embodiments, the treatment sites are located at the river mouth (FIG. 1E). In some embodiments, the treatment sites are located as shown in FIG. 1E: a) for conditions where the carbon capture strategy is to have part of all of the carbonation weathering reactions occurring in the target inland waterbody, and for conditions where the alkalinity status is low or transition; b) for conditions where the carbon capture strategy is to have part of all of the carbonation weathering reactions occurring in the target inland waterbody, and for conditions where a low or transition alkalinity waterbody flows into a transition or high alkalinity waterbody; c) for conditions where the carbon capture strategy is to have most of the carbonation weathering reactions occurring in a reactor and for conditions where the alkalinity status of the waterbodies connecting the addition site with the target inland waterbody mouth are transition or high alkalinity, and d) for conditions where the carbon capture strategy is to have most of the carbonation weathering reactions occurring in the target inland waterbody and for where the alkalinity status of the waters connecting the addition site and the target inland waterbody mouth is transition or high.|[0235] In some embodiments, the treatment site is located at the outflow of the reactor. Examples of locating the treatment site at the outflow of the reactor include estuaries with high alkalinity, weathering reactions taking place inside a reactor, with high target inland waterbody discharge such that it is difficult to detect a change in concentration of carbon variables, or in other cases where it is difficult to detect a change in concentration of carbon variables.|[0236] In some embodiments, the baseline conditions are estimated in the inland waters connecting the addition site with the river mouth. In some embodiments, the baseline conditions are estimated using modelling. In some embodiments, the baseline conditions are estimated using direct observations, or a combination of direct observations and modelling.|[0237] In some embodiments, when the weathering reactions occur in the reactor, the baseline conditions are established from the target inland waterbody chemistry directly upstream of the reactor, or inflow to reactor if using water from the target inland waterbody for the reaction.|[0238] In some embodiments, when the weathering reactions occur in the target inland waterbody, the control sites and treatment sites are tested to establish pre-treatment values for one or more of the carbon variables, ecological variables and water variables, the pre-treatment data from the control sites and the treatment sites are tested and the models/relationship between treatment and control sites are established to enable future prediction of baseline conditions at treatment sites.|[0239] In some embodiments, the change in the carbon variables at the monitoring site(s) is calculated by comparing the difference between the treatment vs baseline values of carbon variables or by multiplying the difference in the carbon variables by the target inland waterbody discharge, for timesteps ranging from one minute to multiple years [as in the example in Equation (5)].|[0240] In some embodiments, the ecological variables are measured to quantify additional ecosystem co-benefits (FIG. 5).|[0241] The following examples of the present disclosure are intended to be illustrative but non-limiting:|(US20250058273)|EXAMPLES|Methods of Removing Atmospheric Carbon Dioxide (CO2)|[0242] Table 1 below illustrates the steps of the method of removing atmospheric carbon dioxide (CO2) in two exemplary target inland water bodies, one of low alkalinity (Acidic river) and one of neutral/high alkalinity (Alkaline/neutral river). The details of each step are provided below. The examples are based on a combination of field observations and modelled data.|TABLE 1 Illustration of the steps of the of the method of removing atmospheric carbon dioxide(CO2) in low alkalinity and neutral/high alkalinity target inland waterbodies. Case ACase BStep (From FIG. 1A)Acidic riverAlkaline/neutral river A. Identify target inlandWest RiverNorth RiverwaterbodyB. Establish addition site(s)Two, in headwaters; alkalineOne, in lower reach; alkalineand select alkaline material tomaterial is crushed dolomitematerial is crushed dolomitebe usedC. Establish pre-treatmentLow alkalinity, low pH,Transition/high alkalinity,alkalinity status. Test targetelevated strong acids: lowneutral/high pH, low stronginland waterbody pre-alkalinity status, andacids; high alkalinity statustreatment at control anddisconnected connectivityand connected connectivitytreatment sitestypetypeD. Establish control sites andUpstream controlUpstream control, baselinebaseline models model as in (FIG. 20)E. Add alkaline material toDoser application of crushedDirect application of dolomiteaddition sitesdolomite following Equation 6following Equation 6 and and values in Table 3Avalues in Table 3CF. Monitor carbon and waterCDR < 0; target not metCDR > 0; target metvariables, calculate CDRG. Adjust application methodModified by pre-treating riverNone neededto achieve targetswater before adding dolomiteH. Recalculate CDRCDR > 0; target achievedCDR remains > 0 with modifications |Step A. Identify Target Inland Waterbody|[0243] Both target inland waterbodies described in this example are well-connected to the Atlantic Ocean, are widely accessible along the drainage network, and both have a hydrological discharge rate suitable for the addition of alkalinity. Case B has favorable water chemistry for carbonation weathering reactions, while Case A does not.|Step B. Test Target Inland Waterbody and Identify One or More Addition Site(s) and Select Alkaline Material to be Used|[0244] For Case A, two addition sites were selected. The longitudinal slope of the river drainage network was obtained from a digital elevation model, and reaches with higher slope suitable for addition sites were identified. Lakes were mapped in the drainage network. The road network was identified and addition sites were located so that they were close to the road network. Potential anthropogenic impacts were examined; no dams or point source pollution outflows were identified. The mean annual discharge was measured from neighbouring hydrometric stations and a watershed model. The channel and floodplain boundaries around the addition sites were mapped. The ecology was examined and the watershed was found to have Atlantic salmon populations. The bedrock type was examined and it was found to be underlain by slate and granite bedrock. Wetland distribution was mapped.|[0245] For Case B, one addition site was selected to be 10 km above the river mouth. The longitudinal slope of the river drainage network was obtained from a digital elevation model and reaches with higher slope suitable for an addition site was identified. Lakes were mapped in the drainage network. The road network was identified and addition sites were located so that they were close to the road network. Potential anthropogenic impacts were examined; no dams or point source pollution outflows were identified. The mean annual discharge and flood frequency analysis was established from neighbouring hydrometric stations and a watershed model. The channel and floodplain boundaries around the addition sites were mapped. The ecology was examined and the watershed was found to have Atlantic salmon populations. The bedrock type was examined and it was found to be underlain by dolomitic limestone. Wetland distribution was mapped.|Step C. Establish Pre-Treatment Alkalinity Status of the Target Inland Waterbody at Control and Treatment Sites Including at River Mouth.|[0246] Case A was tested and found to have low alkalinity, low pH (mean pH was 4.7) and elevated strong acids (e.g., DOC concentrations of 15 mg/L). Its alkalinity status was found to be “low”, and pre-treatment connectivity status was determined to be “disconnected” (as in FIG. 1C). Case B was tested and found to have high alkalinity, high pH (mean pH of 7.4), and low strong acids (e.g., DOC concentrations of less than 5 mg/L); its alkalinity status was found to be “high” and pre-treatment connectivity status was determined to be “connected” (as in FIG. 1C).|Step D. Establish Models Between Control and Treatment Sites to Enable Future Prediction of Baseline Values.|[0247] Case A was tested and it was determined to set control sites directly upstream of both addition sites, and have three treatment sites, one below the weathering zone, one at the river mouth, and one between the two sites. The connectivity type below the addition site was determined to be disconnected (FIG. 1C, case d, disconnected).|[0248] Case B was tested and it was determined to set control sites directly upstream of the addition site and to set the treatment sites at the outflow of the addition site and at the river mouth, considering the connected status of the drainage waters (following FIG. 1C, case c, connected).|[0249] Baseline values were calculated as follows: first, a pre-treatment relation was established between a river-mouth treatment site (T) and the control site (C) (e.g., FIG. 20A). In this example for Case B, the relation was a linear model between bicarbonate concentrations at the control and treatment sites where T=1.34C+1.05, where units are μmol/L. Following application of the alkaline amendment, the baseline values were calculated from the control values, using the model established pre-treatment (FIG. 20B).|Step E. Add Alkaline Material to Addition Sites, Following the Initial Alkaline Material Addition Method|[0250] Case A: The initial method for the addition of alkaline materials for Case A was done via automated lime dosing at two locations in the upper watershed, using method for improving fish habitat in acidic rivers, by dosing to achieve target pH instead of target CDR. These dosers were situated such that turbulent waters were immediately downstream of the addition sites in order to increase rates of weathering reactions and maximize dissolution. Dosing rates of crushed dolomitic limestone ranged between 880 and 7900 mg/m3 and accounted for the dissolution of the product (Table 3A). Total dosing amounts are 23 tonnes of dolomite over the study period. Purity of the dolomite was monitored via laboratory analyses. Depending on river gradient and the hydrology of the watershed, the optimal method to distribute alkalinity may be: (a) automated lime dosers situated along a drainage network, (b) the addition of alkaline material directly to headwater lakes, or (c) a combination of the two approaches. The CDR strategy for Case A is to increase both the carbonation weathering rates by adding dolomite and to increase the alkalinity to increase retention of HCO3− in the river downstream of the addition site to the river mouth.|[0251] Case B: Alkaline materials for Case B were added via automated lime dosing, using the same infrastructure as for Case A, at a location in a lower reach of the watershed. Dosing rates of crushed dolomitic limestone ranged between 880 and 7814 mg/m3 and accounted for the dissolution of the product (Table 3A). Total dosing amounts are 230 tonnes of dolomite over the study period. Purity of the dolomite was monitored via laboratory analyses. The CDR strategy for Case B was to increase carbonation weathering rates only as the alkalinity downstream is already high.|Alkaline Material|[0252] The alkaline material used in both Case A and Case B examples was dolomitic limestone CaMg(CO3)2 with approximately 40% calcium and 33% magnesium, by weight.|Step F. Monitor Water and Carbon Variables and Calculate CDR|[0253] The results for the control and treatment sites for both Case A and B were examined (Tables 2 and 3 and FIG. 18). Baseline values were calculated from control data using the relation between the control and treatment sites established during the pre-treatment phase (FIG. 20). At the control and treatment sites, pCO2, pH, water temperature, salinity and discharge were measured, and HCO3 was calculated using the program CO2SYS (Lewis and Wallace, 1998) (Table 3). Bicarbonate concentration differences between the treatment and baseline values at the river mouth were multiplied by discharge at the river mouth on a daily timestep to quantify the increase in bicarbonate export flux [Equation (5)]. From this increase in bicarbonate export flux the amount of carbon added in the dolomite amendment and the amount of grey emissions were subtracted [Equation (4)]. The CDR totals were then summed for the period of interest (Table 2).|[0254] Table 2 provides CDR calculations for the Case A initial alkaline amendment application method (Step F) and improved alkaline amendment application method (Step H), and for Case B, initial and final alkaline amendment application. Cases were modelled for 43-day periods for scenarios based on observed data. All masses are in metric tonnes (t) of CO2e. d=day. C is the increase in HCO3 delivery to ocean. I is amount of carbon added in alkaline amendment. G is carbon expended in grey emissions. CDR_gross does not account for grey emissions. CDR_net does account for grey emissions. Totals are the summed masses over the 43-day period. Potential carbon drawdown from increased ocean alkalinity was not considered here (as in FIG. 19).|TABLE 2 CDR calculations. CASE A STEP FCASE A STEP HCASE B  Mean Mean Mean TotaldailyTotaldailyTotaldaily tt/dtt/dtt/d  C2.30.04959.71.31563.39I10.60.2310.60.231082.3CDR_GROSS−8.1−0.1849.31.0750.01.09G1.6 1.6 1.6CDR_NET−9.7 47.7 48.3 |[0255] In Case A, for Step F, the CDR was negative (FIG. 18A, Table 2). The CDR value was negative because the increase in CO2e at the river mouth was less than the CO2e added via the dolomite. Thus, additions of the carbonate alkaline amendment increased CO2 emissions rather than drawing down CO2. Comparison of the DIC above (KRC) and below the weathering zones (KRT in FIG. 6, following schema in FIG. 1E) showed that the presence of strong acids impaired carbonation weathering, thus releasing CO2 [Equation (3)] instead of sequestering CO2 [Equation (1)]. Further, the low pH in the river below the weathering zone also caused a loss of HCO3−; while pH and HCO3− increased through the weathering zone, the increases were not maintained all the way to the river mouth (FIG. 8). Thus, because CDR was negative, the target was not met.|[0256] For Case B. CDR was found to be positive (FIG. 18C, Table 2), reaching the CDR target.|[0257] CDR for Case B can also be calculated from the amount of alkaline material added multiplied by carbonation weathering stoichiometry and efficiency factors [Equation (7)]. In this example summed for the study period, D=230 t dolomite, F=0.48, E=0.40, and G=1.6 tCO2e, resulting in a CDR_gross of 46 tCO2e and CDR_net of 44 tCO2e.|Step G. Adjust Alkaline Amendment Method to Achieve Targets.|[0258] For Case A, because the CDR target was not met, the alkaline amendment application method was modified by adding a non-carbonate based alkaline amendment before the dolomite was added, neutralizing the strong acids allowing carbonation weathering of the dolomite, and increasing the alkalinity in the drainage waters leading from the addition sites to the river mouth. In addition to allowing carbonation weathering reactions to take place in the weathering zone, the addition of a non-carbonate-based alkaline amendment elevated the pH to above 6.3 through the drainage network to the river mouth allowing increased amounts of HCO3− to be delivered to the ocean, thus ensuring a continuous length of favorable water chemistry from the addition site to the ocean.|[0259] Other methods which can be used to increase CDR in acidic rivers with a negative CDR are: the introduction of a reactor where pCO2 levels are elevated, using microbial catalysts for carbonation weathering, and increasing the application of dolomite rate to increase pH in weathering zone.|Step H. Continue Monitoring Carbon and Water Variables and Calculating CDR. Re-Adjust Alkaline Amendment Addition Method if Needed.|[0260] As a result of the change in the alkaline amendment application method for Case A, monitoring of the treatment and baseline values showed that CDR was positive (Table 2 Case A Step H and FIG. 18B). Thus, with the adjustments in Step G, Case A had the CDR in the target zone (Step H in Table 1). Ongoing monitoring of baseline, treatment, and control data, and making adjustments to amendment method were performed so that CDR remains in target values over the long-term.|Step I. Document Ecosystem Co-Benefits|[0261] Following the process outlined in FIG. 5, in Case A, environmental co-benefits of the process were determined. One ecological co-benefit was increasing pH above 6.5 from a previous value of 4.7, so that pH levels meet water quality standards. Another ecological co-benefit was the reduction toxic ionic aluminum to below toxic threshold levels. Another ecological co-benefit was the increased calcium concentrations to meet water quality levels. Both Case A and Case B will also have the ecological co-benefit of contributing to reduced ocean acidification by adding alkalinity to coastal zones (FIG. 19).|Data Used to Demonstrate Methods|[0262] The following data were modelled for a 43-day period based on observations for Case A and Case B. Here the treatment monitoring site in all cases was at the river mouth.|[0263] CDR(DL) represents daily gross carbon dioxide removal (not including grey emissions). CDR(CLT) represents cumulative daily gross carbon dioxide removal through the study period. C represents the difference in bicarbonate flux at the river mouth [following Equation (5)]. I represents the amount of carbon input in the alkaline amendment (in tonnes CO2e). HCO3-t represents the bicarbonate concentration at the treatment monitoring site during the study period in μmol/kg [following Equation (5)]. HCO3-b represents the bicarbonate concentration for baseline conditions at the treatment monitoring site during the study period in μmol/kg. Baseline conditions were modelled from control, following the example method in FIG. 20, and following Equation (5). pHt represents the pH at the treatment monitoring site during the study period. pHb represents the pH for baseline conditions at the treatment monitoring site during the study period. Baseline conditions were modelled from control following the example method in FIG. 20. Q represents the river discharge at the river mouth during the study period, in m3/day [following Equation (5)]. D represents the mass of alkaline amendment added in kg/day. Here only the mass of the dolomitic material was included. Mass of the non-carbonate based alkaline amendment used in Case A step H was not included in this total. gaa is the prescribed dose of alkaline material per unit river discharge; here in this ratio only the dolomitic material was included.|TABLE 3A Case A data for initial alkaline material addition method (Step F in FIG. 1A). CDR (DL)CDR (CLT)CIHCO3-tHCO3-b  QDgaaDatet-CO2et-CO2et-CO2et-CO2eμmol/kgμmol/kgpH-tpH-bm3/daykg/daymg/m3 16 Jun. 2022−0.17−0.170.060.237.41.14.84.7223,336500224017 Jun. 2022−0.19−0.360.040.237.41.54.84.7163,861500305018 Jun. 2022−0.01−0.370.030.237.41.94.84.7137,331500364019 Jun. 2022−0.2−0.560.030.237.41.74.84.7123,236500406020 Jun. 2022−0.18−0.750.050.237.41.34.84.7170,208500294021 Jun. 2022−0.12−0.870.110.237.31.24.84.7423,594500118022 Jun. 2022−0.16−1.030.070.237.31.54.84.7263,599500190023 Jun. 2022−0.18−1.210.050.237.31.34.84.7201,647500248024 Jun. 2022−0.18−1.380.050.237.31.34.84.7201,647500248025 Jun. 2022−0.2−1.580.030.237.31.44.84.7127,047500394026 Jun. 2022−0.2−1.780.030.237.21.54.84.7115,685500432027 Jun. 2022−0.2−1.980.030.237.21.94.84.7117,504500426028 Jun. 2022−0.2−2.180.030.237.22.14.84.7128,382500389029 Jun. 2022−0.2−2.380.030.237.32.34.84.7145,794500343030 Jun. 2022−0.15−2.530.050.237.21.94.84.7195,94050025501 Jul. 2022−0.19−2.720.040.237.21.74.84.7176,34150028402 Jul. 2022−0.1−2.820.130.237.21.94.84.7561,9065008903 Jul. 2022−0.1−2.910.130.237.21.84.84.7565,2605008804 Jul. 2022−0.19−3.10.040.237.21.84.84.7175,39250028505 Jul. 2022−0.19−3.290.040.237.224.84.7186,62450026806 Jul. 2022−0.19−3.480.040.237.12.24.84.7175,30950028507 Jul. 2022−0.2−3.680.030.237.22.24.84.7134,78450037108 Jul. 2022−0.2−3.880.030.237.22.64.84.7172,86250028909 Jul. 2022−0.15−4.020.080.237.12.54.84.7411,684500121010 Jul. 2022−0.16−4.180.070.237.12.54.84.7330,098500151011 Jul. 2022−0.19−4.380.040.237.12.44.84.7192,906500259012 Jul. 2022−0.19−4.570.040.237.11.54.84.7147,254500340013 Jul. 2022−0.18−4.750.050.237.11.44.84.7207,668500241014 Jul. 2022−0.19−4.930.040.237.01.74.84.7190,380500263015 Jul. 2022−0.2−5.130.030.237.01.94.84.7148,843500336016 Jul. 2022−0.21−5.340.020.237.11.94.84.794,919500527017 Jul. 2022−0.21−5.550.020.237.12.24.84.794,704500528018 Jul. 2022−0.22−5.760.010.237.02.34.84.763,391500789019 Jul. 2022−0.22−5.980.010.237.02.44.84.762,822500796020 Jul. 2022−0.2−6.180.030.237.11.94.84.7123,302500406021 Jul. 2022−0.18−6.360.050.237.21.84.84.7218,342500229022 Jul. 2022−0.19−6.550.040.237.21.84.84.7172,800500289023 Jul. 2022−0.2−6.740.030.237.22.14.84.7149,277500335024 Jul. 2022−0.2−6.940.030.237.12.44.84.7143,741500348025 Jul. 2022−0.2−7.140.030.237.11.84.84.7151,286500330026 Jul. 2022−0.16−7.30.070.237.11.94.84.7317,862500157027 Jul. 2022−0.13−7.430.10.237.11.94.84.7423,391500118028 Jul. 2022−0.15−7.580.080.237.224.84.7368,091500136029 Jul. 2022−0.17−7.740.060.237.32.34.84.7291,724500171030 Jul. 2022−0.17−7.910.060.237.32.44.84.7269,018500186031 Jul. 2022−0.18−8.10.050.237.42.54.84.7224,3925002230 |TABLE 3B Case A data for modified alkaline material addition method, where an additionalnon-carbonate alkaline material was added to the process (Step H in FIG. 1A). CDR (DL)CDR (CLT)CIHCO3-tHCO3-b  QDgaaDatet-CO2et-CO2et-CO2et-CO2eμmol/kgμmol/kgpH-tpH-bm3/daykg/daymg/m3 16 Jun. 20221.841.842.070.23210.706.714.67223336500223917 Jun. 20221.333.181.560.23216.406.734.67163861500305118 Jun. 20220.733.910.960.23158.506.594.67137331500364119 Jun. 20220.984.891.210.23222.706.754.67123236500405720 Jun. 20221.26.091.430.23190.606.694.67170208500293821 Jun. 20222.88.893.020.23162.106.634.67423594500118022 Jun. 20221.810.692.020.23174.406.684.68263599500189723 Jun. 20221.5412.231.770.23199.506.754.69201647500248024 Jun. 20221.1513.381.380.23155.306.674.69201647500248025 Jun. 20220.5713.950.80.23142.706.654.69127047500393626 Jun. 20220.4814.430.70.23138.106.654.69115685500432227 Jun. 20220.7215.150.950.23183.106.794.69117504500425528 Jun. 20220.5715.720.790.23140.606.674.71128382500389529 Jun. 20220.516.210.720.23112.506.584.7145794500342930 Jun. 20221.2617.471.480.2317206.764.719594050025521 Jul. 20220.7918.261.020.23131.206.624.717634150028352 Jul. 20223.121.363.320.23134.406.634.695619065008903 Jul. 20223.6725.033.90.23156.806.694.695652605008854 Jul. 20221.2226.251.450.23187.406.774.6917539250028515 Jul. 20220.827.051.020.23124.406.594.6918662450026796 Jul. 20221.0628.111.290.23167.406.734.6917530950028527 Jul. 20220.6528.760.870.23147.106.674.6913478450037108 Jul. 20220.8129.571.040.23136.906.654.6917286250028929 Jul. 20222.2631.832.490.23137.306.674.69411684500121510 Jul. 20221.9233.762.150.23148.106.724.68330098500151511 Jul. 20221.24351.470.23172.906.794.69192906500259212 Jul. 20220.6435.650.870.23134.406.694.69147254500339513 Jul. 20220.6636.310.890.2397.106.544.68207668500240814 Jul. 20220.937.21.120.23133.906.714.69190380500262615 Jul. 20220.5137.710.740.23112.606.644.68148843500335916 Jul. 20220.1637.870.380.239206.564.794919500526817 Jul. 20220.3338.20.550.23132.706.744.794704500528018 Jul. 20220.1338.330.360.23128.706.754.7163391500788819 Jul. 20220.1538.480.370.23135.206.814.7362822500795920 Jul. 20220.2138.680.430.2379.806.614.73123302500405521 Jul. 20220.7139.390.930.239706.724.72218342500229022 Jul. 20220.6840.070.910.23119.806.844.74172800500289423 Jul. 20220.4440.510.670.23101.706.84.74149277500334924 Jul. 20220.3640.870.580.2392.106.744.74143741500347825 Jul. 20220.4441.310.660.2399.706.784.74151286500330526 Jul. 20220.8842.191.110.2379.106.644.74317862500157327 Jul. 20221.4243.611.650.2388.406.654.73423391500118128 Jul. 2022245.612.230.23137.406.864.74368091500135829 Jul. 20221.5247.121.740.23135.806.834.73291724500171430 Jul. 20221.348.421.520.23128.706.774.73269018500185931 Jul. 20220.8749.291.10.23110.906.684.722243925002228 |TABLE 3C Case B data for the sold alkaline material addition method (Step F in FIG. 1A). CDR (DL)CDR (CLT)CIHCO3-tHCO3-b  QDgaaDatet-CO2et-CO2et-CO2et-CO2eμmol/kgμmol/kgpH-tpH-bm3/daykg/daymg/m3 16 Jun. 20221.341.343.642.3137.6102.17.527.4723333605000214317 Jun. 20221.382.723.682.3152.8104.87.547.4717386105000287618 Jun. 20220.963.683.262.3156.9101.37.527.4713333105000375019 Jun. 20220.944.623.242.3160.8103.47.537.4712823605000389920 Jun. 20221.315.933.612.3147.5100.47.527.4717420805000287021 Jun. 20221.747.674.042.3126.0104.57.537.4742759405000116922 Jun. 20221.258.923.552.3134.5104.47.537.4826859905000186223 Jun. 20220.439.362.732.3135.2104.97.547.4920464705000244324 Jun. 20221.1510.513.452.3141.2102.77.537.4920364705000245525 Jun. 20220.6111.122.912.3152.1102.47.537.4913304705000375826 Jun. 20220.8211.943.122.3166.1104.27.537.4911468505000436027 Jun. 20220.5912.542.892.3159.2104.27.537.4911950405000418428 Jun. 20220.6213.162.922.3154.7104.57.537.5113238205000377729 Jun. 20220.8914.053.192.3154.3103.97.537.514379405000347730 Jun. 20221.5415.593.842.3147.2102.67.537.51959400500025521 Jul. 20220.5816.172.882.3140.0103.37.537.51783410500028042 Jul. 20222.3618.534.662.3124.0105.17.547.49558906050008953 Jul. 20222.2620.794.562.3117.799.47.517.49568260050008804 Jul. 20220.5821.372.882.3144.0106.27.547.491733920500028845 Jul. 20220.5721.942.872.3129.895.57.497.491896240500026376 Jul. 20220.5822.522.882.3140.1103.47.537.491783090500028047 Jul. 20220.3822.902.682.3144.099.97.517.491377840500036298 Jul. 20220.5423.442.842.3137.8100.77.527.491738620500028769 Jul. 20221.4924.933.792.3116.195.17.497.4940968405000122010 Jul. 20222.5527.484.852.3127.194.27.497.4833509805000149211 Jul. 20221.4728.953.772.3145.3100.67.527.4919190605000260512 Jul. 20221.1630.113.462.3156.3104.37.537.4915125405000330613 Jul. 20220.7630.873.062.3144.0109.97.567.4820366805000245514 Jul. 20220.6631.532.962.3138.6103.97.537.4919338005000258615 Jul. 20220.4832.012.782.3150.0107.87.557.4814984305000333716 Jul. 20220.2432.252.542.3167.9108.97.557.59791905000510617 Jul. 20220.2432.492.542.3171.6111.37.567.59570405000522418 Jul. 20220.0932.582.392.3198.9114.07.577.516399105000781419 Jul. 20220.1132.692.412.3199.2116.17.587.536582205000759620 Jul. 20220.4033.092.702.3162.1113.47.577.5312630205000395921 Jul. 20220.9033.993.202.3148.3115.57.587.5222134205000225922 Jul. 20220.6234.612.922.3148.7110.77.567.5417480005000286023 Jul. 20221.2735.883.572.3166.0112.47.577.5415127705000330524 Jul. 20221.2437.123.542.3168.6113.87.577.5414674105000340725 Jul. 20221.2938.413.592.3165.7112.57.577.5415328605000326226 Jul. 20222.9141.325.212.3147.6110.87.567.5432186205000155327 Jul. 20223.8645.196.162.3143.5110.37.567.5342139105000118728 Jul. 20221.5546.733.852.3133.9110.17.567.5436609105000136629 Jul. 20221.2147.943.512.3137.9110.87.567.5329472405000169730 Jul. 20221.1549.093.452.3143.9115.17.587.5327201805000183831 Jul. 20220.9350.023.232.3148.1115.87.587.52227392050002199 |Additional Detail on Methods|Lime Dosers|[0264] Automated lime dosers using common programmable logistic controller (PLC) automation to monitor sensor data (e.g., water level, stream chemical conditions, supply levels, etc.) were used. Initial algorithms to interpret incoming data (e.g., estimating river discharge from water level data and determining appropriate dosing rate), and communicating operations to a centralize, offsite monitoring station were used, and then amended in Step H (FIG. 1A) to include CDR feedback.|Monitoring of Instream Chemical Conditions|[0265] The monitoring of carbon and water variables needed to calculate CDR [discharge, pCO2 or CO2 concentration, temperature, conductivity and pH via Equation (4)], used water chemistry sensors that monitor these variables continuously (e.g., every 5 min or every hour) and are commercially available (FIG. 7).|[0266] A unique algorithm to determine the type, dose and frequency of material to be applied at each alkaline amendment addition site was developed, as a real-time function of water discharge, temperature, and chemistry. An iterative dosing method based on CDR calculations obtained by sensing CO2 concentration, pH, temperature, and conductivity and discharge was used, so that CDR targets could be monitored, using Equations (4), (5) and (7). Dose amounts were recorded for CDR calculations in tonnes/day [variable D in Equation (7)]. Chemical concentration of the dolomite alkaline amendments was tracked. Discharge was measured in 15-minute increments to obtain mass flux calculations from concentration data [Equation (5)].|[0267] A method to add extra alkalinity in conditions where the pH is less than 4.5 was developed.|[0268] A method to add extra alkalinity in conditions where strong acids interfered with carbonation weathering was developed.|[0269] A method to add extra alkalinity in conditions where the pH is less than 6.3 was developed.|[0270] A method to add extra alkalinity in conditions where the pH is greater than 6.3 was developed.|[0271] The methods to add extra alkalinity are: 1) change the dosing algorithm to increase the amount of alkaline material added per unit time, 2) reduce loss of alkalinity by adding the alkaline reactant to the water in a reactor, where the water pH is raised to target levels before being released to the river, and 3) adding another addition point upstream of the existing addition point where non-carbonate mineral-based alkaline amendment were added to raise the pH and to remove the strong acids from solution.|[0272] Microbial amendment to increase carbonation weathering rates was used.|Headwater Lake|[0273] When alkalinity was added directly to headwater lakes, the amount, timing and frequency of additions was based on the collection of detailed bathymetric data, limnological characterizations of each lake with specific attention to stratification schedules, and consideration of lake discharge rates. Access to lakes for logistics, such as emersion of a specialized liming barge or the delivery of alkaline material was a parameter taken into consideration.|Monitoring Conditions|[0274] Temperature, pH, carbon variables, HCO3−, pCO2, and/or CO2 concentrations downstream in a transect from the doser site down to the river mouth, or within the lake basin and downstream to the river mouth were monitored. The carbonate system was calculated from these measurements using CO2SYS. When the conditions in the river at the doser were identified as being outside carbonation weathering conditions for the material being used, the river was treated with alkaline material. For example, for limestone: conditions should optimally be pH>4.5 and pCO2>1.0 atm for carbonation weathering to occur, in the absence of strong acids. In Case A, Step F (FIG. 1A) for the initial alkaline material application method, it has been found that the presence of strong acids and low pH were causing CDR<0. In Step G (FIG. 1A) of Case A the alkaline material application method alteration was modified such that when the doser was used, a signal to upstream dosers was sent to increase the input of alkalinity by adding a non-carbonate based alkaline amendment to raise pH to >6.5 to avoid loss of CO2 from the system allow carbonation weathering to occur when the dolomite was added at the second doser. The presence of strong acids is common in acidic rivers and those high proportion of peatlands/wetlands in the watershed, or in the presence of pyritic slate in the watershed (Lehmann et al., 2022).|[0275] This situation, where the conditions were outside carbonation weathering conditions may have occurred because of the presence of strong acids, flood conditions, or during snowpack melt events. Conditions where a reverse reaction (precipitation of CaCO3) may occur (e.g., very high Ca2+ or HCO3− levels) were monitored. Concentrations of pCO2 were monitored to ensure primary production was not limited by lowered CO2 concentrations due to increased pH.|[0276] The following conditions were accounted for CO2 drawdown: the mass of alkaline amendment applied and reaction stoichiometry [I in Equation (4)]; differences in treated and baseline carbon variables values; and pH of waters downstream of dosing site(s) to the ocean. Carbon drawdown was calculated using Equations (4), (5) and/or (7). Metals and water chemistry was monitored to ensure no unintended negative consequences occur.|Field Measurement of Carbon Concentration and Carbon Fluxes|[0277] The experimental infrastructure consisted of control monitoring stations and treatment monitoring stations (FIG. 6). All stations measured carbon variables and water variables at control sites upstream of lime dosers and treatment sites downstream of lime dosers in two rivers (Killag and West) (Killag River is show in FIG. 6). The red star represents the addition site and the circles represent upstream and downstream monitoring sites (control and treatment sites, respectively). AF_WR is the river mouth.|[0278] The monitoring stations consisted of a CO2 concentration sensor (eosGP unit) to measure CO2 concentration, which is then converted to pCO2 values, a pH and temperature sensor (HOBO MX2501 unit), a conductivity sensor, and an optional CO2 Flux Sensor (eosFD unit) to measure CO2 flux (FIG. 7). Continuous monitoring to collect data for the modelling took place from June 23 to Dec. 1, 2021. All stations were sited in calm-water areas to reduce signal noise associated with stream turbulence. CO2SYS was used to calculate the values of variables in the carbonate system from the measured values.|[0279] Two roving stations were used for transects, and short and longer-term spot checks to determine the extent of acidification of rivers in the region. Roving stations were assemblages of sensors similar to that used in permanent stations but modified to permit transportation between sites. Modifications included the removal of anchors, a reduction in the size and buoyancy of floats or mounting of the equipment to the bow or gunnels of watercraft.|[0280] To map patterns of CO2 flux downstream from the lime doser to estimate the carbon sequestration in the oceans, a transect of a 9 km reach down the Killag River to the ocean was conducted. On Sep. 8, 2021, an eosFD unit was carried downstream from just above the Killag River lime doser to a location approximately 9 kilometers downstream of the doser, collecting a 20-minute flux measurement every kilometer.|[0281] To further understand the range of carbon fluxes in untreated rivers in the region, CO2 fluxes were measured at 84 short-term (30-60 minutes) and seven long-term (3-5 days) measurements with the eosFD unit at sites across Nova Scotia in September-November 2021. The average CO2 flux ranged from −0.07 to 7.11 at sites outside the exemplary embodiments in Nova Scotia (FIG. 9, 16, 17).|Stream Chemistry Sampling|[0282] During the experimental period, 20 grab sampling events took place at the control and treatment sites on the Killag River and 15 grab sampling events took place at the control and treatment sites on the West River. The collected samples were analyzed for water chemistry including alkalinity and partial pressure of carbon dioxide (pCO2).|[0283] At each site visit, in-situ measurements of pH, water temperature, and specific conductance were collected side-by-side at the permanent stations, for quality analysis/quality assurance, using a handheld YSI Pro10 multiparameter water quality meter. This unit was calibrated immediately before sampling.|[0284] Grab samples to be analyzed for metals' content were collected using sterilized polyethylene syringes into sterilized polyethylene tubes (15 mL). These samples were filtered in the field and preserved with nitric acid (HNO3) within a week of arriving at the laboratory. Dissolved metals were measured by passing the sample through a 0.45 um polyethersulfone (PES) filter. Organic metals were measured by passing a filtered sample through a 3 cm negatively charged cation exchange column (Bond Elut Jr. Strong Cation Exchange Column). Grab samples to be analyzed for water chemistry parameters including total organic carbon (TOC) and alkalinity were not filtered and were collected in sterilized amber glass bottles (1 L). All samples were kept cooled to a temperature of 4° C. during transport to the lab and were delivered to the lab within 48 hours of being collected.|[0285] Samples to be analyzed for pCO2 were collected in triplicate using sterilized polyethylene syringes and stopcocks into sterilized glass headspace vials (20 mL). Vials were sealed with no headspace using a hand crimper and aluminum seals with flat butyl septa. Samples were preserved with mercuric chloride (HgCl2) and kept cooled to a temperature of 4° C. prior to analysis.|[0286] Samples to be analyzed for alkalinity were collected in 250-mL glass media bottles. Samples were preserved with mercuric chloride (HgCl2) and stored at room temperature prior to analysis.|Results|Confirmation that the Addition of Alkalinity Reduces CO2 Fluxes|[0287] Field testing demonstrated that addition of alkalinity reduces CO2 fluxes. CO2 flux was significantly higher at the control sites (KRC and WRC) than the treatment sites (KRT and WRT) in both Killag and West rivers (FIGS. 10, 11, 12, Table 3).|[0288] Field testing demonstrated that the addition of alkalinity reduces CO2 concentration and pCO2. CO2 concentration was significantly higher at the control sites (KRC and WRC) than at the treatment sites (KRT and WRT) in both Killag and West rivers (FIGS. 13, 14, 15, Table 1).|TABLE 3 Median values for water chemistry parameters at control and treatmentsites for the 2021 measurement period. All differences between controland treatment sites are statistically significant (p < 0.0001).  CO2 fluxCO2 concentration  Site(μm ol m−2 s−1)(ppm)pH   KRC0.4623514.66 KRT0.135526.49 WRC0.5416284.32 WRT0.168796.36  |Environmental Conditions Altering CO2 Flux|[0289] Decreasing pH was significantly correlated with increasing CO2 flux at all permanent stations. The relationship was stronger at the control sites in both rivers (FIGS. 11A and 11B).|[0290] Increasing water temperature increased the difference in CO2 flux between the control and treatment sites in the Killag river (FIG. 12A). In the West River the relationship was less clear, as lower temperatures had high spikes of CO2 flux, which may be associated with flushing of cold water from the lake upstream during flood events (FIG. 12B).|Effect of Liming on River CO2 Concentrations|[0291] Liming significantly reduced aqueous CO2 concentrations, which were significantly higher at the control sites than at the treatment sites (FIGS. 13A and 13B, Table 3).|[0292] Liming significantly increased HCO3 concentrations, which were significantly higher downstream of the addition sites (FIG. 8).|Effects of Environmental Parameters on CO2 Concentration|[0293] Increasing pH significantly reduced CO2 concentration (FIGS. 14A and 14B), along the range of pH at the four sites.|[0294] Increasing water temperature significantly increased aqueous CO2 concentration at the untreated sites. The sites treated with liming do not have an increase in CO2 flux with increasing temperature (FIGS. 15A and 15B).|Patterns of CO2 Flux in Untreated Rivers Across Acidified Areas of Nova Scotia|[0295] The average CO2 flux ranged from 0.22 to 3.15 at longer-term float sites (FIG. 16B) and ranged from −0.07 to 7.11 at the spot-check float sites (FIG. 9, 16A). CO2 flux was significantly higher with lower pH across the longer-term and spot check float sites (FIG. 17).|[0296] While the above description provides examples of one or more apparatuses or methods, it will be appreciated that other apparatuses or methods may be within the scope of the accompanying claims.|FULL CITATIONS FOR DOCUMENTS REFERRED TO IN THE SPECIFICATION|- Bach, L. T., Gill, S. J., Rickaby, R. E., Gore, S., & Renforth, P. 2019. CO2 removal with enhanced weathering and ocean alkalinity enhancement: potential risks and co-benefits for marine pelagic ecosystems. Frontiers in Climate, 1, 7.|- Beerling, D. J., Leake, J. R., Long, S. P., Scholes, J. D., Ton, J., Nelson, P. N., Bird, M., Kantzas, E., Taylor, L. L. and Sarkar, B.: Farming with crops and rocks to address global climate, food and soil security, Nature plants, 1, 2018.|- Beerling, D. J., Kantzas, E. P., Lomas, M. R., Wade, P., Eufrasio, R. M., Renforth, P., . . . & Banwart, S. A. 2020. Potential for large-scale CO 2 removal via enhanced rock weathering with croplands. Nature, 583(7815), 242-248.|- Berner, Robert A., and Antonio C. Lasaga. Modeling the geochemical carbon cycle. Scientific American 260.3 (1989): 74-81.|- Bertagni, Matteo B., and Amilcare Porporato. The Carbon-Capture Efficiency of Natural Water Alkalinization: Implications For Enhanced weathering. Science of The Total Environment 838 (2022): 156524.|- Fawzy, S., Osman, A. I., Doran, J., & Rooney, D. W. 2020. Strategies for mitigation of climate change: a review. Environmental Chemistry Letters, 1-26.|- Hamilton, S. K., Kurzman, A. L., Arango, C., Jin, L. and Robertson, G. P.: Evidence for carbon sequestration by agricultural liming, Global Biogeochem. Cycles, 21, 2007.|- Jens Hartmann, A. Joshua West, Phil Renforth, Peter Köhler, Christina L. De La Rocha, Dieter A. Wolf-Gladrow, Hans H. Darr, and Jürgen, Enhanced chemical weathering as a geoengineering strategy to reduce atmospheric carbon dioxide, supply nutrients, and mitigate ocean acidification, Reviews of Geophysics, 51/2013.|- Horgby, Å., Segatto, P. L., Bertuzzo, E., Lauerwald, R., Lehner, B., Ulseth, A. J., . . . & Battin, T. J. 2019. Unexpected large evasion fluxes of carbon dioxide from turbulent streams draining the world's mountains. Nature communications, 10(1), 1-9.|- IPCC, 2018: Climate Change 2018: The Physical Science Basis. Contribution of Working Group I to the Fifth Assessment Report of the Intergovernmental Panel on Climate Change [Masson-Delmotte, Cambridge University Press.|- IPCC, 2021: Climate Change 2021: The Physical Science Basis. Contribution of Working Group I to the Sixth Assessment Report of the Intergovernmental Panel on Climate Change [Masson-Delmotte, V., P. Zhai, A. Pirani, S. L. Connors, C. Péan, S. Berger, N. Caud, Y. Chen, L. Goldfarb, M. I. Gomis, M. Huang, K. Leitzell, E. Lonnoy, J. B. R. Matthews, T. K. Maycock, T. Waterfield, O. Yelekçi, R. Yu, and B. Zhou (eds.)]. Cambridge University Press. In Press.|- Kantola, I. B., Masters, M. D., Beerling, D. J., Long, S. P. and DeLucia, E. H.: 2017. Potential of global croplands and bioenergy crops for climate change mitigation through deployment for enhanced weathering, Biology letters, 13, 20160714, 2017.|- Kokic, J., M. B. Wallin, H. E. Chmiel, B. A. Denfeld, and S. Sobek (2015), Carbon dioxide evasion from headwater systems strongly contributes to the total export of carbon from a small boreal lake catchment, J. Geophys. Res. Biogeosci., 120, doi:10.1002/2014JG002706.|- Lehmann, Nele, et al. Alkalinity generation from carbonate weathering in a silicate-dominated headwater catchment at Iskorasfjellet, northern Norway. Biogeosciences Discussions (2022): 1-39.|- Lewis, E., and D. W. R. Wallace. CO2SYS-Program developed for the CO2 system calculations. Carbon Dioxide Inf Anal Center Report ORNL/CDIAC-105 (1998).|- Middelburg, J. J., Soetaert, K., and Hagens, M. (2020), Understanding alkalinity to quantify ocean buffering, Eos, 101, https://doi.org/10.1029/2020EO146562. Published on 29 Jul. 2020.|- Mook, W., and Kazimierz Rozanski. Environmental isotopes in the hydrological cycle. IAEA Publish 39 (2000). Chapter 9.|- Mumma, H., et al., 2022, Continuous Monitoring of Net CO2 Drawdown from Experimental Ocean Alkalinity Additions, A G U, 2022.|- Renforth, P., & Henderson, G. (2017). Assessing ocean alkalinity for carbon sequestration. Reviews of Geophysics, 55(3), 636-674.|- Terlouw, T., Bauer, C., Rosa, L. and Mazzotti, M., 2021. Life cycle assessment of carbon dioxide removal technologies: a critical review. Energy & Environmental Science, 14(4), pp. 1701-1721.|- Uroz, S., Calvaruso, C., Turpault, M. P., & Frey-Klett, P. (2009). Mineral weathering by bacteria: ecology, actors and mechanisms. Trends in microbiology, 17(8), 378-387.|- Wallin, M. B., Grabs, T., Buffam, I., Laudon, H., Agren, A., Öquist, M. G., & Bishop, K. 2013. Evasion of CO2 from streams—The dominant component of the carbon export through the aquatic conduit in a boreal landscape. Global Change Biology, 19(3), 785-797. Family Number|(105522431)|105522431|Abstract|(WO2023115224 A1)|L'invention concerne des procédés d'élimination du dioxyde de carbone dans les eaux continentales et une augmentation de l'alcalinité dans les océans. Les procédés peuvent comprendre l'ajout d'une ou plusieurs matières alcalines à un ou plusieurs sites d'ajout dans une quantité suffisante pour permettre l'amélioration de l'altération, conduisant à l'élimination nette du dioxyde de carbone de l'atmosphère.|Methods for carbon dioxide removal in inland waters and increased delivery of alkalinity to oceans. Methods can include adding one or more alkaline materials to one or more addition sites in an amount effective to enable enhanced weathering to occur, leading to net carbon dioxide removal from the atmosphere.|(CN118660865 A)|Methods for carbon dioxide removal in inland waters and increasing basicity to the ocean are disclosed . The methods may include adding one or more basic materials to one or more addition sites in an amount effective to enable enhanced weathering to occur to achieve net carbon dioxide removal from the atmosphere . |(EP4452871 A4)|Methods for carbon dioxide removal in inland waters and increased delivery of alkalinity to oceans. Methods can include adding one or more alkaline materials to one or more addition sites in an amount effective to enable enhanced weathering to occur, leading to net carbon dioxide removal from the atmosphere.|(IN202417047811 A)|Methods for carbon dioxide removal in inland waters and increased delivery of alkalinity to oceans. Methods can include adding one or more alkaline materials to one or more addition sites in an amount effective to enable enhanced weathering to occur, leading to net carbon dioxide removal from the atmosphere.|(US20250058273 A1)|Methods for carbon dioxide removal in inland waters and increased delivery of alkalinity to oceans. Methods can include adding one or more alkaline materials to one or more addition sites in an amount effective to enable enhanced weathering to occur, leading to net carbon dioxide removal from the atmosphere.|(CA3242169 A1)|Methods for carbon dioxide removal in inland waters and increased delivery of alkalinity to oceans. Methods can include adding one or more alkaline materials to one or more addition sites in an amount effective to enable enhanced weathering to occur, leading to net carbon dioxide removal from the atmosphere.(From US2025058273 A1)|CPC codes|(WO2023115224 A1)|B01D-053/62|B01D-053/78|B01D-2251/30|B01D-2251/402|B01D-2251/404|B01D-2257/504|B01D-2258/06|B01D-2259/45|G01N-033/18/2|(CN118660865 A)|B01D - 053/62 |(EP4452871 A4)|B01D-053/62|B01D-053/78|B01D-2251/30|B01D-2251/402|B01D-2251/404|B01D-2257/504|B01D-2258/06|B01D-2259/45|G01N-033/18/2|(US20250058273 A1)|B01D-053/62|B01D-053/78|B01D-2251/30|B01D-2251/402|B01D-2251/404|B01D-2257/504|B01D-2258/06|B01D-2259/45|G01N-033/18/2|(CA3242169 A1)|B01D-053/62|B01D-053/78|B01D-2251/30|B01D-2251/402|B01D-2251/404|B01D-2257/504|B01D-2258/06|B01D-2259/45|G01N-033/18/2|IPC codes|(WO2023115224 A1)|B01D-019/04|B01D-053/62|G01N-033/18|(BR112024012757 A2)|B01D-019/04|B01D-053/62|G01N-033/18|(CN118660865 A)|B01D - 019/04 |B01D - 053/62 |G01N - 033/18 |(EP4452871 A4)|B01D-019/04|B01D-053/62|G01N-033/18|(IN202417047811 A)|C01F-017/32|(US20250058273 A1)|B01D-053/62|B01D-053/78|(CA3242169 A1)|B01D-019/04|B01D-053/62|G01N-033/18|Title|(WO2023115224 A1)|Methods of carbon dioxide removal in freshwater|(BR112024012757 A0)|Methods of carbon dioxide removal in freshwater|(EP4452871 A1)|Methods of carbon dioxide removal in freshwater|(EP4452871 A4)|Methods of carbon dioxide removal in freshwater|(IN202417047811 A)|Methods of carbon dioxide removal in freshwater|(US20250058273 A1)|Methods of carbon dioxide removal in freshwater|(CA3242169 A1)|Methods of carbon dioxide removal in freshwater| Analysis of biological materials|Basic materials chemistry|Chemical engineering|Civil engineering|Environmental technology|Materials, metallurgy B01D-053/62|B01D-053/78|B01D-2251/30|B01D-2251/402|B01D-2251/404|B01D-2257/504|B01D-2258/06|B01D-2259/45|C02F-001/00/1|C02F-001/28/3|C02F-001/40|C02F-001/52|C02F-001/56|C02F-001/66|C02F-001/68|C02F-001/78|C02F-003/02|C02F-003/32|C02F-003/32/7|C02F-003/34|C02F-003/34/7|C02F-007/00|C02F-009/00|C02F-011/00|C02F-2001/007|C02F-2103/001|C02F-2103/007|C02F-2103/08|C02F-2201/008|C02F-2209/003|C02F-2209/005|C02F-2209/02|C02F-2209/06|C02F-2209/22|C02F-2209/40|C02F-2301/08|C02F-2303/16|E02B-001/00|E02B-003/00|E02B-015/06|E02F-001/00|G01N-033/18/2|Y02C-010/04|Y02C-020/40 B01D-053/62|B01D-053/78|B01D-2251/30|B01D-2251/402|B01D-2251/404|B01D-2257/504|B01D-2258/06|B01D-2259/45|C02F-001/00/1|C02F-001/28/3|C02F-001/40|C02F-001/52|C02F-001/56|C02F-001/66|C02F-001/68|C02F-001/78|C02F-003/02|C02F-003/32|C02F-003/32/7|C02F-003/34|C02F-003/34/7|C02F-007/00|C02F-009/00|C02F-011/00|C02F-2001/007|C02F-2103/001|C02F-2103/007|C02F-2103/08|C02F-2201/008|C02F-2209/003|C02F-2209/005|C02F-2209/02|C02F-2209/06|C02F-2209/22|C02F-2209/40|C02F-2301/08|C02F-2303/16|E02B-001/00|E02B-003/00|E02B-015/06|E02F-001/00|G01N-033/18/2|Y02C-010/04|Y02C-020/40 B01D-019/04|B01D-053/62|B01D-053/78|C01F-017/32|C02F-001/66|C02F-001/68|C04B-040/02|C10K-001/00|E02B-003/00|G01N-033/18 B01D-019/04|B01D-053/62|B01D-053/78|C01F-017/32|C02F-001/66|C02F-001/68|C04B-040/02|C10K-001/00|E02B-003/00|G01N-033/18 WO2025166357|WO2025178742|WO2025259881|US12448309|GB2636851|CN117390884B WO2025166357 115547774 WHO=Examiner SELF=N CAT=Y|WO2025178742 115724494 WHO=Examiner SELF=N CAT=X CAT=I|WO2025259881 116993845 WHO=Examiner SELF=N CAT=I|US12448309 115724494 WHO=Applicant SELF=N|GB2636851 108540140 WHO=Examiner SELF=N|CN117390884B 108145906 WHO=Examiner SELF=N US20140229392|US20140229392|CN102351300|CN102351300|GB2447513|GB2447513|US20130292344|WO202450337 US20140229392 64760084 WHO=Examiner SELF=N CAT=Y|US20140229392 64760084 WHO=Examiner SELF=N CAT=Y|CN102351300 7559934 WHO=Examiner SELF=N CAT=Y|CN102351300 7559934 WHO=Examiner SELF=N CAT=Y|GB2447513 17863068 WHO=Examiner SELF=N CAT=Y|GB2447513 17863068 WHO=Examiner SELF=N CAT=Y|US20130292344 14306973 WHO=Examiner SELF=N CAT=X CAT=I|WO202450337 108748980 WHO=Examiner SELF=N CAT=E XP093077459; XP093077490; GB2447513; US20140229392; XP093077501; CN102351300; XP093077503||GB2447513; US20140229392; CN102351300; WO202450337; US20130292344; XP037220195|||| (EP4452871)|Search Report references [Examiner]|-BENTHAUS FRIEDRICH-CARL ET AL: "In-lake Neutralization of East German Lignite Pit Lakes: Technical History and New Approaches from LMBV", MINE WATER AND THE ENVIRONMENT, SPRINGER BERLIN HEIDELBERG, BERLIN/HEIDELBERG, vol. 39, no. 3, 23 July 2020 (2020-07-23), pages 603 - 617, XP037220195, ISSN: 1025-9112, [retrieved on 20200723], DOI: 10.1007/S10230-020-00707-5|-See also references of WO 2023115224A1|||(WO2023/115224)|International Search Report [Examiner]|-GOMEZ FABIAN A. ET AL: "Increasing River Alkalinity Slows Ocean Acidification in the Northern Gulf of Mexico", THE 3RD EAA EUROPEAN CONGRESS ON ACOUSTICS (FORUM ACUSTICUM 2002), JOHN WILEY &amp; SONS, INC., SEVILLA, SPAIN, vol. 48, no. 24, 28 December 2021 (2021-12-28), Sevilla, Spain , pages 1 - 9, XP093077459, ISSN: 0094-8276, DOI: 10.1029/2021GL096521|-BURT DANIEL J., FRÖB FRIEDERIKE, ILYINA TATIANA: "The Sensitivity of the Marine Carbonate System to Regional Ocean Alkalinity Enhancement", FRONTIERS IN CLIMATE, vol. 3, pages 1 - 15, XP093077490, DOI: 10.3389/fclim.2021.624075|-RENFORTH P., CAMPBELL J. S.: "The role of soils in the regulation of ocean acidification", PHILOSOPHICAL TRANSACTIONS. ROYAL SOCIETY OF LONDON. B: BIOLOGICAL SCIENCES., ROYAL SOCIETY, LONDON., GB, vol. 376, no. 20200174, 27 September 2021 (2021-09-27), GB , pages 1 - 10, XP093077501, ISSN: 0962-8436, DOI: 10.1098/rstb.2020.0174|-BACH LENNART T., BOYD PHILIP W.: "Seeking natural analogs to fast-forward the assessment of marine CO 2 removal", PROCEEDINGS OF THE NATIONAL ACADEMY OF SCIENCES, NATIONAL ACADEMY OF SCIENCES, vol. 118, no. 40, 5 October 2021 (2021-10-05), pages 1 - 8, XP093077503, ISSN: 0027-8424, DOI: 10.1073/pnas.2106147118|-See also references of EP 4452871A4||||| PENDING (EP4452871)|PENDING|(US20250058273)|PENDING|(WO2023/115224)|LAPSED|(CN118660865)|PENDING|(IN202417047811)|PENDING|(BR112024012757)|PENDING|(CA3242169)|PENDING ALIVE (EP4452871)|ALIVE|(US20250058273)|ALIVE|(WO2023/115224)|DEAD|(CN118660865)|ALIVE|(IN202417047811)|ALIVE|(BR112024012757)|ALIVE|(CA3242169)|ALIVE (EP4452871)|LEGAL DETAILS FOR EP4452871|Actual or expected expiration date=2042-12-23|Legal state=ALIVE|Status=PENDING|Event publication 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STATUS EVENT CODE: A-1-1-A10-A00-A102 (AS PROVIDED BY THE NATIONAL OFFICE)|Event text: COMPLIANCE REQUIREMENTS DETERMINED MET|Effective date of the event=2024-07-02|Event publication date=2024-07-02|Event code=CA/P18|Event group=Corrections|PRIORITY CLAIM ADDED OR AMENDED|ST27 STATUS EVENT CODE: A-1-1-P10-P18-P105 (AS PROVIDED BY THE NATIONAL OFFICE)|Event text: PRIORITY CLAIM REQUIREMENTS DETERMINED COMPLIANT|Effective date of the event=2024-07-02|Event publication date=2024-07-02|Event code=CA/W00|Event group=Administrative notifications|OTHER EVENT OCCURRED|ST27 STATUS EVENT CODE: A-1-1-W10-W00-W100 (AS PROVIDED BY THE NATIONAL OFFICE)|Event text: LETTER SENT|Effective date of the event=2024-07-02 (EP4452871)|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR|(WO2023/115224)|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW|(WO2023/115224)|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ|(WO2023/115224)|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR|(WO2023/115224)|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML|(WO2023/115224)|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (EP4452871)|EP; SE|(US20250058273)|US|(WO2023/115224)|BR; CA; CN; EP; IN; US|(CN118660865)|CN|(IN202417047811)|IN|(BR112024012757)|BR|(CA3242169)|CA https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=ECLncZT9nTUVTAjFdm1K+3mXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022555265&ekey=2043&xpn=EP4452871&kind=A4 https://register.epo.org/application?number=EP22908981 https://permalink.orbit.com/RenderStaticFirstPage?XPN=5p8oUjmKxPMuw56Xk6cpNXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT US (WO2023/115224)|CA (WO2023/115224)|NAME=CARBONRUN CARBON DIOXIDE REMOVAL LIMITED 600-1741 Lower Water Street Halifax, Nova Scotia B3J 0J2 , COUNTRY=CA (EP4452871)|GB|(WO2023/115224)|CA||(CA3242169)|CA (EP4452871)|NAME=Dehns;St. Bride's House 10 Salisbury Square , CITY=London EC4Y 8JD , COUNTRY=GB , REG=101728904|(WO2023/115224)|NAME=BERESKIN & PARR LLP/S.E.N.C.R.L., S.R.L. 40 King Street West 40th Floor Toronto, Ontario M5H 3Y2 , POSTCODE=M5H 3Y2 , COUNTRY=CA|(CN118660865)|NAME=ZHANG ZHENGZHENG;CHINA PAT INTELLECTUAL PROPERTY OFFICE , REG=11270NAME=LI XUE;CHINA PAT INTELLECTUAL PROPERTY OFFICE , REG=11270|(CA3242169)|NAME=SMART & BIGGAR LP SCOTIA PLAZA 40 KING ST W, 40TH FLOOR , CITY=TORONTO , POSTCODE=M5H 3Y2 , COUNTRY=CA , REG=2800 |(EP4452871)|CA; CA|(US20250058273)|CA; CA|(WO2023/115224)|CA; CA||||(CA3242169)|CA; CA (EP4452871)|NAME=STERLING, Shannon|NAME=HALFYARD, Edmund A.|(EP4452871)|NAME=STERLING, Shannon, CITY=Halifax, Nova Scotia B3H 2A8, COUNTRY=CA |NAME=HALFYARD, Edmund A., CITY=Middle Sackville, Nova Scotia B4E 0M9, COUNTRY=CA|(US20250058273)|NAME=Sterling Shannon, CITY=Halifax, COUNTRY=CA |NAME=Halfyard Edmund A., CITY=Middle Sackville, COUNTRY=CA|(WO2023/115224)|NAME=STERLING, Shannon 6738 Jubilee Road Halifax, Nova Scotia B3H 2A8, POSTCODE=B3H 2A8, COUNTRY=CA |NAME=HALFYARD, Edmund A. 163 McCabe Lake Drive Middle Sackville, Nova Scotia B4E 0M9, POSTCODE=B4E 0M9, COUNTRY=CA|(CN118660865)|NAME=SHANNON STERLING|NAME=HUFYARD EDMUND A|(IN202417047811)|NAME=Sterling Shannon|NAME=Halfyard Edmund A|(BR112024012757)|NAME=STERLING SHANNON|NAME=HALFYARD EDMUND A|(CA3242169)|NAME=HALFYARD EDMUND A. 163 McCabe Lake Drive, CITY=MIDDLE SACKVILLE, POSTCODE=B4E 0M9, COUNTRY=CA |NAME=STERLING SHANNON 6738 Jubilee Road, CITY=HALIFAX, POSTCODE=B3H 2A8, COUNTRY=CA 18 7 Titre: (EP4452871)|Methods of carbon dioxide removal in freshwater Résumé: (EP4452871)|Methods for carbon dioxide removal in inland waters and increased delivery of alkalinity to oceans. Methods can include adding one or more alkaline materials to one or more addition sites in an amount effective to enable enhanced weathering to occur, leading to net carbon dioxide removal from the atmosphere. 20 Abstract gpt-4o-mini yes The article discusses methods for carbon dioxide removal through enhanced weathering by adding alkaline materials, which aligns with the definition of accelerated weathering and carbon sequestration.
19 CN202410031450 CN202410031450 CN117861518 109351414 CN117861518 A 2024-04-12 [CN117861518] 2024-01-09 2024-01-09 2024-04-12 (CN117861518)|2044-01-09 (CN117861518)|Industrial solid waste two-stage carbon sequestration device and method (CN117861518)|The invention provides an industrial solid waste two-stage carbon sequestration device and method. The industrial solid waste two-stage carbon sequestration device comprises a mixing mechanism; the first carbon sequestration reaction mechanism comprises a first reaction bin, a material conveyor and a plurality of airflow amplifiers; the communicating mechanism comprises a communicating pipe and a crusher; and the second carbon sequestration reaction mechanism comprises a second reaction bin, a first gas inlet assembly, a second gas inlet assembly and a plurality of spray guns. The cement decomposition kiln tail gas is subjected to physical adsorption and chemical absorption through the first carbon sequestration reaction mechanism and the second carbon sequestration reaction mechanism, CO2 in the cement decomposition kiln tail gas can be subjected to sufficient carbon sequestration, on one hand, the overall carbon sequestration process has the remarkable advantages of being high in matching degree, good in carbon sequestration effect, high in automation degree and the like, and meanwhile, the carbon sequestration effect is good. The carbon-fixed steel slag micro-powder after carbon fixation does not have the stability problem of steel slag, has higher activity and wear resistance, and can be recycled, so that the carbon-fixed steel slag micro-powder has excellent actual use value and wide use prospect. SUZHOU SHIJING TECHNOLOGY (CN117861518)|SUZHOU SHIJING TECHNOLOGY CO., LTD. ([CN]) LU SHOUJIANG|XIN FENG|CHENG XINAN|DONG SHIHONG|WU QIANQIAN|HE WEN (CN117861518)|LU SHOUJIANG|XIN FENG|CHENG XINAN|DONG SHIHONG|WU QIANQIAN|HE WEN (CN117861518)|FENG RUI;CENTRAL SOUTH WELL INTELLECTUAL PROPERTY OFFICE|Reg. Nb: 32257 (CN117861518)|A large amount of calcium magnesium oxide in the steel slag can be used for capturing CO 2 The higher reactivity and the inherent alkalinity of the carrier make it more suitable for mineralizing CO 2 Mineralizing and sealing CO by utilizing steel slag 2 Not only can lighten CO 2 The discharge pressure of the steel slag can also improve the recycling utilization rate of the steel slag, and the mineralized steel slag has stable structure and can be better applied to the fields of building materials, roadbed materials and the like, so how to recycle the steel slag and combine the steel slag with a carbon fixation technology is a great direction of the development of the industry.|Compared with the prior art, the technical scheme of the invention has the following advantages: according to the industrial solid waste two-stage carbon fixing device and method, the first carbon fixing reaction mechanism and the second carbon fixing reaction mechanism are used for carrying out physical adsorption and chemical absorption on the tail gas of the cement decomposing kiln, so that CO in the tail gas of the cement decomposing kiln can be absorbed 2 On the one hand, the carbon fixing device is arranged through reasonable structural layout and an internal creative carbon fixing mechanism, so that the whole carbon fixing process has the remarkable advantages of high matching degree, good carbon fixing effect, high automation degree and the like, on the other hand, the carbon fixing slag micro powder after carbon fixing has no stability problem of steel slag, has higher activity and wear resistance, can be used as a novel carbon fixing high-quality mixed material for cement production, and can also be used for preparing high-efficiency carbon fixing composite admixture by synergic preparation of other low-price industrial solid wastes, thereby being capable of replacing mineral powder and reducing clinker consumption in cement production, further replacing mineral powder in concrete production, improving concrete performance quality and reducing cement consumption.|The industrial solid waste two-stageThe carbon fixing device performs physical adsorption and chemical absorption on the tail gas of the cement decomposing kiln through the first carbon fixing reaction mechanism 200 and the second carbon fixing reaction mechanism 400, and can perform physical adsorption and chemical absorption on CO in the tail gas of the cement decomposing kiln 2 On one hand, the method has the remarkable advantages of high cooperation degree, good carbon fixing effect, high automation degree and the like in the whole carbon fixing process, and on the other hand, the steel slag micro powder after carbon fixing has no stability problem, has higher activity and wear resistance, can be used as a novel carbon fixing high-quality mixed material for cement production, and can also be used as a novel carbon fixing high-efficiency composite admixture for preparing other low-price industrial solid wastes in a synergistic manner, thereby being capable of replacing mineral powder and reducing clinker consumption in cement production, and simultaneously, the steel slag micro powder after carbon fixing can also replace mineral powder in concrete production, improve concrete performance quality and reduce cement consumption.| (CN117861518)|1. The utility model provides an industry solid useless two-stage solid carbon device which characterized in that: comprising the following steps:a mixing mechanism;a first carbon sequestration reaction mechanism comprising: the material conveying device comprises a first reaction bin, a material conveyor and a plurality of air flow amplifiers, wherein the first reaction bin is communicated with the mixing mechanism, the material conveyor is arranged inside the first reaction bin, and the air flow amplifiers are communicated with the first reaction bin;the communicating mechanism comprises a communicating pipe and a crusher, one end of the communicating pipe is communicated with the first reaction bin, and the crusher is arranged inside the communicating pipe;a second carbon sequestration reaction mechanism comprising: the device comprises a second reaction bin, a first air inlet component, a second air inlet component and a plurality of spray guns, wherein the second reaction bin is communicated with the other end of the communicating pipe, the spray guns, the first air inlet component and the second air inlet component are all communicated with the second reaction bin, the first air inlet component faces to the outlet of the second reaction bin, and the second air inlet component is arranged at the bottom of the second reaction bin.| (CN117861518)|In order to solve the technical problems, the invention provides an industrial solid waste two-stage carbon fixing device, which comprises: a mixing mechanism; a first carbon sequestration reaction mechanism comprising: the material conveying device comprises a first reaction bin, a material conveyor and a plurality of air flow amplifiers, wherein the first reaction bin is communicated with the mixing mechanism, the material conveyor is arranged inside the first reaction bin, and the air flow amplifiers are communicated with the first reaction bin; the communicating mechanism comprises a communicating pipe and a crusher, one end of the communicating pipe is communicated with the first reaction bin, and the crusher is arranged inside the communicating pipe; a second carbon sequestration reaction mechanism comprising: the device comprises a second reaction bin, a first air inlet component, a second air inlet component and a plurality of spray guns, wherein the second reaction bin is communicated with the other end of the communicating pipe, the spray guns, the first air inlet component and the second air inlet component are all communicated with the second reaction bin, the first air inlet component faces to the outlet of the second reaction bin, and the second air inlet component is arranged at the bottom of the second reaction bin.|The invention provides an industrial solid waste two-stage carbon fixing device and method, comprising the following steps: a mixing mechanism; a first carbon sequestration reaction mechanism comprising: a first reaction bin, a material conveyor, and a plurality of air flow amplifiers; a communication mechanism including a communication pipe and a crusher; a second carbon sequestration reaction mechanism comprising: the device comprises a second reaction bin, a first air inlet assembly, a second air inlet assembly and a plurality of spray guns.|The invention relates to the field of carbon dioxide emission reduction treatment, in particular to an industrial solid waste two-stage carbon fixing device and method.| (CN117861518)|CARBON FIXING(100,80)|REACTION BIN(100,30)|SOLID WASTE(100,28)|TWO STAGE CARBON FIXING(100,26)|CARBON(100,3)|INDUSTRY SOLID(100,1)|CEMENT TAIL GAS(50,9)|STEEL SLAG(41,21)|CRUSHER(37,5)|REACTION BIN OUTLET(37,2)|REDUCING CLINKER CONSUMPTION(34,2)|SPRAY GUN(32,5)|AIR INLET COMPONENT(31,28)|TAIL GAS(30,9)|CARBON SEQUESTRATION(30,8)|CARRIER ALKALINITY(27,1)|CEMENT PRODUCTION(26,10)|INORGANIC POWDER(24,8)|COMPOSITE ADMIXTURE(23,1)|AIR INLET(22,7)|REPLACING MINERAL POWDER(22,2)|KILN(21,9)|CARBON SEQUESTRATION REACTION(21,7)|SLAG MICRO POWDER(21,4)|STEEL SLAG MICRO POWDER(21,4)|REDUCING CEMENT CONSUMPTION(21,1)|CONCRETE PERFORMANCE QUALITY(20,4)|COMMUNICATION PIPE(20,3)|SYNERGIC(19,1)|MIXING BIN(18,10)|CONCRETE PRODUCTION(18,5)|STEEL SLAG STABILITY(18,3)|CARBON FIXING COMPOSITE ADMIXTURE(18,1)|CONVEYER EQUIPMENT(17,9)|LAYOUT STRUCTURE(17,2)|INDUSTRIAL WASTE SEQUESTRATION(17,1)|MIXED CARBON FIXING(16,36)|REACTIVITY(16,1)|PHYSICAL ADSORPTION(15,6)|SUSPENSION FLUIDIZATION(15,4)|INTERNAL CREATIVE CARBON FIXING(15,1)|LINKAGE(14,9)|GASEOUS MATTER(14,8)|COOPERATION DEGREE(14,2)|AIR FLOW AMPLIFIER(13,6)|REACTION BED(13,4)|ABUNDANT SOLID CARBON(13,1)|RECYCLING UTILIZATION RATE(13,1)|DISCHARGE VALVE(12,15)|SPEED REDUCER(12,6)|AUTOMATION DEGREE(12,4)|LIQUID ACTIVATION CATALYST DOPING(12,2)|MIROPOWDER(12,1)|SLAG STEEL MASS(11,3)|DOPING MASS(11,2)|WEAR ABILITY(11,1)|CARBON FIXING REACTION(10,23)|EMISSION REDUCTION TREATMENT(10,1)|CARBON FIXATION(9,10)|ECCENTRIC SHAFT(9,8)|AIR INLET PIPE(9,6)|ROADBED MATERIAL(9,1)|SOLID MATTER(8,10)|CYCLONE DUST REMOVAL(8,5)|LIQUID CATALYST ACTIVATION(8,4)|WEAR RESISTANCE(8,3)|CHIMNEY(7,5)|NAOH SOLUTION(7,4)|BEARING SUPPORT SEAT(7,2)|CARBON FIXING(7,2)|MATCH DEGREE(7,2)|MICRO POWDER(7,2)|AIRFLOW AMPLIFIER(6,3)|CLINKER CONSUMPTION(6,3)|LIMESTONE GYPSUM(6,2)|SMOKE EMISSION(6,2)|CALCIUM MAGNESIUM OXIDE(6,1)|PROCESSING TEMPERATURE(5,8)|PRIMARY CARBON FIXING(5,4)|AIR VALVE ADJUSTMENT(5,2)|BEARING SEAT SUPPORT(5,2)|WIDE APPLICATION PROSPECT(5,1)|ACETIC ACID(4,7)|CARBON DIOXIDE(4,6)|HUNDRED MILLION TON(4,2)|DESULFURIZATION GYPSUM ADDITION(4,1)|DESULPHURIZED GYPSUM(4,1)|DISCHARGE PRESSURE(4,1)|GLOBAL INDUSTRIAL EMISSION(4,1)|SMOKE DUST EMISSION(4,1)|WHOLLY SOLID CARBON(4,1)|HIGH EFFICIENCY COMPOSITE ADMIXTURE(3,4)|SOLID CARBON STEEL(3,3)|SYNERGISM(3,3)|CARBON FIXATION REACTION(3,2)|GRIND ABILITY(3,2)|AMERICAN LECO(3,1)|CARBON DIOXIDE FIELD(3,1)|CEMENT CONSUMPTION(3,1)|CLOTH BAG DUST COLLECTION(3,1)|CONCRETE ADMIXTURE(3,1)|CYCLONE DUST COLLECTION(3,1)|EXTENSIVE UTILIZATION(3,1)|MICRO CRACK(3,1)|SILICATE CEMENT CLINKER(3,1)|STEEL SLAG YIELD(3,1)|CARBON CONTENT(2,2)|CARBON DIOXIDE EMISSION(2,2)| (CN117861518)|1. The invention provides an industry solid useless two-stage solid carbon device which characterized in that: comprising the following steps:|a mixing mechanism;|a first carbon sequestration reaction mechanism comprising: the material conveying device comprises a first reaction bin, a material conveyor and a plurality of air flow amplifiers, wherein the first reaction bin is communicated with the mixing mechanism, the material conveyor is arranged inside the first reaction bin, and the air flow amplifiers are communicated with the first reaction bin;|the communicating mechanism comprises a communicating pipe and a crusher, one end of the communicating pipe is communicated with the first reaction bin, and the crusher is arranged inside the communicating pipe;|a second carbon sequestration reaction mechanism comprising: the device comprises a second reaction bin, a first air inlet component, a second air inlet component and a plurality of spray guns, wherein the second reaction bin is communicated with the other end of the communicating pipe, the spray guns, the first air inlet component and the second air inlet component are all communicated with the second reaction bin, the first air inlet component faces to the outlet of the second reaction bin, and the second air inlet component is arranged at the bottom of the second reaction bin.|2. The industrial solid waste two-stage carbon fixing device according to claim 1, wherein: the first carbon fixation reaction mechanism further comprises a temperature control assembly, and the temperature control assembly is connected with the first reaction bin.|3. The industrial solid waste two-stage carbon fixing device according to claim 1, wherein: the mixing mechanism comprises a mixing bin and a first discharge valve, the mixing bin is communicated with the first reaction bin, the first discharge valve is arranged at the discharge end of the mixing bin, the communication mechanism further comprises a second discharge valve, and the second discharge valve is arranged at the discharge end of the communication pipe.|4. The industrial solid waste two-stage carbon fixing device according to claim 1, wherein: the second carbon-fixing reaction mechanism further comprises a reaction bed and a third discharge valve, and the first air inlet component and the third discharge valve are respectively arranged at two ends of the reaction bed.|5. The industrial solid waste two-stage carbon fixing device according to claim 1, wherein: the first air inlet assembly comprises a first air inlet pipe; the second air inlet assembly comprises a plurality of second air inlet pipes and a plurality of adjusting air valves, wherein the second air inlet pipes correspond to each other one by one.|6. The industrial solid waste two-stage carbon fixing device according to claim 1, wherein: the auxiliary mechanism comprises a base and at least one shaking assembly, wherein the shaking assembly is arranged on the base and comprises a bearing seat, a speed reducer, a linkage assembly and an eccentric shaft, the bearing seat supports the second carbon-fixing reaction mechanism, one end of the eccentric shaft is connected with the bearing support seat, the other end of the eccentric shaft is connected with the linkage assembly, and the linkage assembly is connected with the speed reducer.|7. The two-stage carbon fixation method for industrial solid waste is characterized by comprising the following steps of: carbon sequestration processing by the industrial waste sequestration device of any one of claims 1 to 6, comprising in particular the following steps:|s1, mixing slag steel, desulfurized gypsum and Na 2 SiO 3 And activating the catalyst in a liquid state to obtain a first mixed carbon-fixing raw material;|s2, mixing the mixed carbon-fixing raw material with CO to be absorbed at a first processing temperature 2 Obtaining a second mixed carbon-fixing raw material after primary carbon fixing;|s3, crushing the second mixed carbon-fixing raw material, and then mixing the crushed second mixed carbon-fixing raw material with NaOH and CO in a suspension fluidization state 2 Reacting to obtain a third mixed carbon-fixing raw material;|s4, recycling the third mixed carbon-fixing raw material.|8. The industrial solid waste two-stage carbon fixing method as claimed in claim 7, wherein: the mixing mass of the desulfurized gypsum in the step S1 is 8-10% of the mass of the slag steel, and the Na is as follows 2 SiO 3 The doping mass is 8% -10% of the slag steel mass, and the ratio of the liquid activation catalyst doping mass to the solid raw material mass is 1:1 to 3:1, wherein the solid raw materials comprise the slag steel, desulfurized gypsum and Na 2 SiO 3 The liquid activated catalyst comprises acetic acid and water, and the volume ratio of the acetic acid to the water is 1: 30-1: 50.|9. the industrial solid waste two-stage carbon fixing method as claimed in claim 8, wherein: in the step S2, the first processing temperature is 60-80 ℃; in the step S3, the concentration of NaOH is 1.8-2.2%, and the ratio of the mass of the NaOH solution to the mass of the solid raw material is 4% -8%; the air supply amount of the first air inlet component is 0.1-0.3 m 3 /h; the air supply amount of the second air inlet component is 2.0-3.0 m 3 /h。|10. The industrial solid waste two-stage carbon fixing method as claimed in claim 7, wherein: the step S4 specifically comprises the following steps: separating gaseous matters and solid matters from the third mixed carbon-fixing raw material after cyclone dust removal and cloth bag dust removal in sequence, and introducing the gaseous matters into a chimney to recycle the solid matters. (CN117861518)|TECHNICAL FIELD|[0001] The invention relates to the field of carbon dioxide emission reduction treatment, in particular to an industrial solid waste two-stage carbon fixing device and method.|BACKGROUND ART|[0002] The cement industry occupies a significant proportion of the global anthropogenic carbon dioxide emissions, about 7% of the global anthropogenic carbon dioxide emissions, and about 12% of the global industrial emissions. According to the 2DS convention of paris protocol in 2015, the global cement industry was required to achieve the goal of carbon neutralization in 2050 and a 40% reduction in carbon was necessary in 2030. The cement yield in 2022 in China is about 21.18 hundred million tons, and if calculated by about 604.7kg of carbon emission per ton of cement counted by China cement institute, the carbon dioxide emitted by the cement industry is about 12.8 hundred million tons. Facing such tremendous carbon emission reduction tasks, the cement industry needs to find new emission reduction routes.|[0003] The carbon dioxide gas generated by the cement industry is converted into carbonate or a new carbon-containing product, and a new direction is provided for carbon emission reduction of the cement industry. Particularly, the industries capable of consuming a large amount of carbon dioxide become support industries for realizing large-scale carbon emission reduction in the cement industry.|[0004] Steel slag is a solid waste produced in the steelmaking process, and the yield of the steel slag is about 15-20% of the yield of coarse steel. However, the actual utilization rate of the steel slag in China is only 30%, a large amount of steel slag is abandoned and piled up, and a large amount of land is occupied. The steel slag contains hydraulic material, and can be used as cementing material to replace silicate cement clinker after being ground. However, steel slag and tailings after treatment thereof have difficulty in large-scale building material utilization. The main reason is that the activity of the steel slag in cement and concrete building materials is low, and the steel slag contains a large amount of free oxides, and the free oxides are easy to expand in volume when meeting water, so that micro cracks appear in the building materials, and the strength is further reduced.|[0005] A large amount of calcium magnesium oxide in the steel slag can be used for capturing CO 2 The higher reactivity and the inherent alkalinity of the carrier make it more suitable for mineralizing CO 2 Mineralizing and sealing CO by utilizing steel slag 2 Not only can lighten CO 2 The discharge pressure of the steel slag can also improve the recycling utilization rate of the steel slag, and the mineralized steel slag has stable structure and can be better applied to the fields of building materials, roadbed materials and the like, so how to recycle the steel slag and combine the steel slag with a carbon fixation technology is a great direction of the development of the industry.|DISCLOSURE|Disclosure of Invention|[0006] Therefore, the invention aims to solve the technical problem of using steel slag in the carbon fixing technology in the prior art and provides an industrial solid waste two-stage carbon fixing device and method.|[0007] In order to solve the technical problems, the invention provides an industrial solid waste two-stage carbon fixing device, which comprises: a mixing mechanism; a first carbon sequestration reaction mechanism comprising: the material conveying device comprises a first reaction bin, a material conveyor and a plurality of air flow amplifiers, wherein the first reaction bin is communicated with the mixing mechanism, the material conveyor is arranged inside the first reaction bin, and the air flow amplifiers are communicated with the first reaction bin; the communicating mechanism comprises a communicating pipe and a crusher, one end of the communicating pipe is communicated with the first reaction bin, and the crusher is arranged inside the communicating pipe; a second carbon sequestration reaction mechanism comprising: the device comprises a second reaction bin, a first air inlet component, a second air inlet component and a plurality of spray guns, wherein the second reaction bin is communicated with the other end of the communicating pipe, the spray guns, the first air inlet component and the second air inlet component are all communicated with the second reaction bin, the first air inlet component faces to the outlet of the second reaction bin, and the second air inlet component is arranged at the bottom of the second reaction bin.|[0008] In one embodiment of the invention, the first carbon-fixing reaction mechanism further comprises a temperature control component, and the temperature control component is connected with the first reaction bin.|[0009] In one embodiment of the invention, the mixing mechanism comprises a mixing bin and a first discharge valve, wherein the mixing bin is communicated with the first reaction bin, the first discharge valve is arranged at the discharge end of the mixing bin, and the communication mechanism further comprises a second discharge valve which is arranged at the discharge end of the communication pipe.|[0010] In an embodiment of the invention, the second carbon-fixing reaction mechanism further comprises a reaction bed and a third discharge valve, and the first air inlet component and the third discharge valve are respectively arranged at two ends of the reaction bed.|[0011] In one embodiment of the invention, the first air intake assembly comprises a first air intake pipe; the second air inlet assembly comprises a plurality of second air inlet pipes and a plurality of adjusting air valves, wherein the second air inlet pipes correspond to each other one by one.|[0012] In one embodiment of the invention, the device further comprises an auxiliary mechanism, wherein the auxiliary mechanism comprises a base and at least one shaking assembly, at least one shaking assembly is arranged on the base and comprises a bearing seat, a speed reducer, a linkage assembly and an eccentric shaft, the bearing seat supports the second carbon fixation reaction mechanism, one end of the eccentric shaft is connected with the bearing support seat, the other end of the eccentric shaft is connected with the linkage assembly, and the linkage assembly is connected with the speed reducer.|[0013] The invention also provides an industrial solid waste two-stage carbon fixing method which is implemented by adopting the industrial solid waste two-stage carbon fixing device,the method specifically comprises the following steps: s1, mixing slag steel, desulfurized gypsum and Na in a mixing mechanism 2 SiO 3 And activating the catalyst in a liquid state to obtain a first mixed carbon-fixing raw material; s2, introducing the mixed carbon-fixing raw material into a first reaction bin, and enabling the mixed carbon-fixing raw material to pass through a material conveyor, a plurality of airflow amplifiers and CO to be absorbed at a first processing temperature 2 Obtaining a second mixed carbon-fixing raw material after primary carbon fixing; s3, crushing the second mixed carbon-fixing raw material, introducing the crushed second mixed carbon-fixing raw material into a second carbon-fixing reaction mechanism, spraying NaOH into the second carbon-fixing reaction mechanism, and providing CO to be absorbed to the second carbon-fixing reaction mechanism from the lateral direction and the bottom through a first air inlet component and a second air inlet component respectively 2 The second mixed carbon-fixing raw material, the NaOH and the CO to be absorbed are in a suspension fluidization state 2 Reacting to obtain a third mixed carbon-fixing raw material; s4, recycling the third mixed carbon-fixing raw material.|[0014] In one embodiment of the present invention, the desulphurized gypsum in the step S1 is doped with 8-10% of the slag steel mass, and the Na is 2 SiO 3 The doping mass is 8% -10% of the slag steel mass, and the ratio of the liquid activation catalyst doping mass to the solid raw material mass is 1:1 to 3:1, wherein the solid raw materials comprise the slag steel, desulfurized gypsum and Na 2 SiO 3 The liquid activated catalyst comprises acetic acid and water, and the volume ratio of the acetic acid to the water is 1: 30-1: 50.|[0015] in one embodiment of the present invention, in step S2, the first processing temperature is 60 to 80 ℃; in the step S3, the concentration of NaOH is 1.8-2.2%, and the ratio of the mass of the NaOH solution to the mass of the solid raw material is 4% -8%; the air supply amount of the first air inlet component is 0.1-0.3 m 3 /h; the air supply amount of the second air inlet component is 2.0-3.0 m 3 /h。|[0016] In one embodiment of the present invention, step S4 specifically includes: separating gaseous matters and solid matters from the third mixed carbon-fixing raw material after cyclone dust removal and cloth bag dust removal in sequence, and introducing the gaseous matters into a chimney to recycle the solid matters.|[0017] Compared with the prior art, the technical scheme of the invention has the following advantages:|[0018] according to the industrial solid waste two-stage carbon fixing device and method, the first carbon fixing reaction mechanism and the second carbon fixing reaction mechanism are used for carrying out physical adsorption and chemical absorption on the tail gas of the cement decomposing kiln, so that CO in the tail gas of the cement decomposing kiln can be absorbed 2 On the one hand, the carbon fixing device is arranged through reasonable structural layout and an internal creative carbon fixing mechanism, so that the whole carbon fixing process has the remarkable advantages of high matching degree, good carbon fixing effect, high automation degree and the like, on the other hand, the carbon fixing slag micro powder after carbon fixing has no stability problem of steel slag, has higher activity and wear resistance, can be used as a novel carbon fixing high-quality mixed material for cement production, and can also be used for preparing high-efficiency carbon fixing composite admixture by synergic preparation of other low-price industrial solid wastes, thereby being capable of replacing mineral powder and reducing clinker consumption in cement production, further replacing mineral powder in concrete production, improving concrete performance quality and reducing cement consumption. Therefore, the method has excellent practical use value, and is a novel industrial solid waste two-stage carbon fixing device and method with wide use prospect.|DRAWINGS DESCRIPTION|[0019] In order that the invention may be more readily understood, a more particular description of the invention will be rendered by reference to specific embodiments thereof that are illustrated in the appended drawings.|[0020] FIG. 1 is a schematic perspective view of an industrial solid waste two-stage carbon fixing device in a preferred embodiment of the invention;|[0021] FIG. 2 is a side view of the industrial waste two-stage carbon fixing device of FIG. 1;|[0022] FIG. 3 is a schematic cross-sectional view taken at A-A of FIG. 2;|[0023] FIG. 4 is a top view of the reaction bed of FIG. 1;|[0024] FIG. 5 is a schematic view of the auxiliary mechanism of FIG. 1;|[0025] FIG. 6 is a bar chart showing the average carbon fixation in the fourth, first and second examples of the present invention.|[0026] Description of the specification reference numerals: 100. a mixing mechanism; 110. a mixing bin; 120. a first discharge valve; 200. a first carbon sequestration reaction mechanism; 210. a first reaction bin; 220. a material conveyor; 230. an air flow amplifier; 300. a communication mechanism; 310. a communicating pipe; 320. a crusher; 330. a second discharge valve; 400. a second carbon fixing mechanism; 410. a second reaction bin; 411. a third discharge valve; 412. a reaction bed; 420. a first air intake assembly; 421. a first air inlet pipe; 430. a second air intake assembly; 431. a second air inlet pipe; 432. adjusting an air valve; 440. a spray gun; 450. a vibration hammer; 500. an auxiliary mechanism; 510. a base; 520. shaking the assembly; 530. a bearing seat; 540. a speed reducer; 550. an eccentric shaft; 560. and a linkage assembly.|INVENTION MODE|Detailed Description|[0027] The present invention will be further described with reference to the accompanying drawings and specific examples, which are not intended to be limiting, so that those skilled in the art will better understand the invention and practice it.|[0028] Example 1|[0029] Referring to fig. 1 to 3, the present embodiment provides an industrial solid waste two-stage carbon fixing device, which includes: a mixing mechanism 100; a first carbon sequestration reaction mechanism 200 comprising: the material mixing device comprises a first reaction bin 210, a material conveyor 220 and a plurality of air flow amplifiers 230, wherein the first reaction bin 210 is communicated with the material mixing mechanism 100, the material conveyor 220 is arranged inside the first reaction bin 210, and the air flow amplifiers 230 are communicated with the first reaction bin 210; a communicating mechanism 300 including a communicating pipe 310 and a crusher 320, wherein one end of the communicating pipe 310 communicates with the first reaction chamber 210, and the crusher 320 is disposed inside the communicating pipe 310; a second carbon sequestration reaction mechanism 400 comprising: the second reaction bin 410, the first air inlet assembly 420, the second air inlet assembly 430 and the plurality of spray guns 440, wherein the second reaction bin 410 is communicated with the other end of the communicating pipe 310, the plurality of spray guns 440, the first air inlet assembly 420 and the second air inlet assembly 430 are all communicated with the second reaction bin 410, the first air inlet assembly 420 faces to the outlet of the second reaction bin 410, and the second air inlet assembly 430 is arranged at the bottom of the second reaction bin 410.|[0030] The industrial solid waste two-stageThe carbon fixing device performs physical adsorption and chemical absorption on the tail gas of the cement decomposing kiln through the first carbon fixing reaction mechanism 200 and the second carbon fixing reaction mechanism 400, and can perform physical adsorption and chemical absorption on CO in the tail gas of the cement decomposing kiln 2 On one hand, the method has the remarkable advantages of high cooperation degree, good carbon fixing effect, high automation degree and the like in the whole carbon fixing process, and on the other hand, the steel slag micro powder after carbon fixing has no stability problem, has higher activity and wear resistance, can be used as a novel carbon fixing high-quality mixed material for cement production, and can also be used as a novel carbon fixing high-efficiency composite admixture for preparing other low-price industrial solid wastes in a synergistic manner, thereby being capable of replacing mineral powder and reducing clinker consumption in cement production, and simultaneously, the steel slag micro powder after carbon fixing can also replace mineral powder in concrete production, improve concrete performance quality and reduce cement consumption. Therefore, the method has excellent practical use value, and is a novel industrial solid waste two-stage carbon fixing device with wide use prospect.|[0031] Referring to fig. 1 to 3, in this embodiment, in the height direction of the apparatus, a mixing mechanism 100, a first carbon fixing reaction mechanism 200, a communication mechanism 300 and a second carbon fixing reaction mechanism 400 are sequentially connected from top to bottom, where the mixing mechanism 100 is used to mix steel slag powder after grinding of thermally braised steel slag in a converter and desulfurized gypsum (the main component is CaSO 4 ·2H 2 O) to produce a mixture capable of mixing with CO in the tail gas of a cement-decomposing kiln 2 Fully reacted carbon-fixing raw material, the first carbon-fixing reaction mechanism 200 is used for CO 2 The first carbon fixation process is performed, the communication mechanism 300 is used for crushing the solid raw material carrying a large amount of steel slag after the first reaction, so that the solid raw material can smoothly enter the second carbon fixation reaction mechanism 400 for operation, and the second carbon fixation reaction mechanism 400 is used for mixing the crushed powder raw material with an alkaline solution such as strong sodium oxide and the like to realize CO 2 Thereby achieving the purpose of fully fixing carbon. The used carbon-fixing product can be used as a mixture to produce low-carbon cement or used as a concrete admixture, therebyRealizing the comprehensive utilization of wastes.|[0032] Referring to fig. 3, the mixing mechanism 100 includes a mixing bin 110 and a first discharge valve 120, where the mixing bin 110 is communicated with the first reaction bin 210, and the first discharge valve 120 is disposed at a discharge end of the mixing bin 110. In this embodiment, the first discharge valve 120 is used to control the discharge amount and the discharge speed in the mixing bin 110. Further, a stirring device is provided in the mixing bin 110.|[0033] Referring to fig. 3, the first carbon-fixing reaction mechanism 200 further includes a housing, and the first reaction chamber 210 is preferably a reaction pipe provided inside the housing, and the housing communicates with the second carbon-fixing reaction mechanism 400, thereby filling the periphery of the first reaction chamber 210 with CO to be absorbed 2 In the first carbon sequestration reaction mechanism 200, the CO to be absorbed 2 The gas flow amplifiers 230 enter the first reaction chamber 210, and further, the gas flow amplifiers 230 are uniformly spaced along the extending direction of the first reaction chamber 210, and the gas flow amplifiers 230 consume a small amount of compressed air to fill the CO to be absorbed outside the first reaction chamber 210 2 The flue gas is guided into the first reaction chamber 210, so that the flue gas concentration of the first reaction chamber 210 is increased, the temperature in the first reaction chamber 210 is increased under the action of the air flow amplifier 230, and at the same time, the carbon-fixing raw material slowly moves forward under the conveying action of the material conveyor 220, thereby absorbing CO 2 Fully react to realize CO in the flue gas 2 Is a primary emission reduction of the fuel. Further, in this embodiment, the first carbon-fixing reaction mechanism 200 further includes a temperature control component, and the temperature control component is connected to the first reaction chamber 210, and further, the material conveyor 220 in this embodiment is preferably a screw conveyor. In addition, in this embodiment, the average temperature range in the first carbon fixing reaction mechanism 200 is kept at 60-80 ℃, and this temperature range can promote the carbon fixing reaction of the carbon fixing raw material, accelerate the carbon fixing reaction process, and improve the carbon fixing efficiency. In particular, the present invention is not limited to the specific kind of temperature control assembly.|[0034] In this embodiment, the communication mechanism 300 further includes a second discharge valve 330, where the second discharge valve 330 is disposed at a discharge end of the communication pipe 310. Further, the second discharge valve 330 in this embodiment can control the discharge amount and the discharge speed of the communication mechanism 300, the carbon-fixing product and the unreacted carbon-fixing raw material discharged from the first carbon-fixing reaction mechanism 200 enter the crusher 320 through the communication pipe 310, and are ground into powder under the action of the crusher 320, the particle size of the micro powder required in this embodiment is about 250-280 mesh, and the micro powder of the ground carbon-fixing product and the unreacted carbon-fixing raw material enter the second carbon-fixing reaction mechanism 400 through the discharge valve.|[0035] Referring to fig. 3 and 4, the second carbon-fixing reaction mechanism 400 further includes a reaction bed 412 and a third discharge valve 411, wherein the first air inlet assembly 420 and the third discharge valve 411 are respectively disposed at two ends of the reaction bed 412, and specifically, the first air inlet assembly 420 includes a first air inlet pipe 421; the second air intake assembly 430 includes a plurality of second air intake pipes 431 and a plurality of air regulating valves 432 in a one-to-one correspondence. In this embodiment, the material entering the second carbon-fixing reaction mechanism 400 through the communication mechanism 300 moves towards the third discharge valve 411 under the action of the first air inlet component 420, and at the same time, the carbon-fixing raw material micropowder forms suspension fluidization under the action of the second air inlet component 430, so that on one hand, the movement process of the material can be smoother, the material is prevented from adhering to the surface of the reaction bed 412, and on the other hand, the arrangement can enlarge the material and the CO to be absorbed 2 Further improving the carbon fixation effect of absorption. Specifically, in the present embodiment, the air volume of the first air intake assembly 420 is set to be 0.1-0.3 m 3 And/h, the air volume of the second air inlet assembly 430 is set to be 2.0-3.0 m 3 And/h. In this embodiment, the plurality of spray guns 440 are uniformly spaced along the moving direction of the material and are used for spraying NaOH solution into the second reaction chamber 410, wherein the NaOH solution is used for mixing with the material and the CO to be absorbed 2 The second air inlet pipes 431 can be independently adjusted through the adjusting air valves 432 to improve the flexibility of the equipment. In addition, in the present embodiment, a plurality of hammers 450 are further provided on the sidewall of the second reaction chamber 410 to prevent powder from being deposited in the second carbon-fixing reactor.|[0036] Referring to fig. 5, the auxiliary mechanism 500 further includes an auxiliary mechanism 500, where the auxiliary mechanism 500 includes a base 510 and at least one shaking assembly 520, at least one shaking assembly 520 is disposed on the base 510, and includes a bearing seat 530, a speed reducer 540, a linkage assembly 560, and an eccentric shaft 550, where the bearing seat 530 supports the second carbon-fixing reaction mechanism 400, one end of the eccentric shaft 550 is connected to the bearing support, the other end is connected to the linkage assembly 560, and the linkage assembly 560 is connected to the speed reducer 540. The auxiliary mechanism 500 in this embodiment includes two shaking assemblies 520 disposed at two ends of the base 510 along the length direction thereof, the shaking assemblies 520 enable shaking of a certain frequency to occur during the operation of the first carbon fixing reaction mechanism 200 and the second carbon fixing reaction mechanism 400, and by continuously shaking, the adhesion of carbon fixing products or unreacted carbon fixing raw materials to the inner surface of the first reaction chamber 210 or the second reaction chamber 410 is prevented, meanwhile, the probability of agglomeration of the materials on the reaction bed 412 is greatly reduced by the shaking assemblies 520, and the shaking assemblies 520 can continuously strip the reactants, impurities and surface passivation layers deposited by adsorption on the solid surface to expose new active surfaces, thereby enhancing the internal diffusion mass transfer rate, continuously shrinking solid particles, increasing the effective contact area of gas and solid, and improving the carbon fixing efficiency of the carbon fixing raw materials. Further, in the auxiliary mechanism 500 of the present embodiment, the eccentric amount of the shaking unit 520 is 12 to 15mm and the rotational speed is 20 to 40 rpm.|[0037] Example two|[0038] The embodiment provides an industrial solid waste two-stage carbon fixing method, which is implemented by adopting the industrial solid waste two-stage carbon fixing device in the first embodiment, and specifically comprises the following steps:|[0039] s1, mixing slag steel, desulfurized gypsum and Na in a mixing mechanism 2 SiO 3 And a liquid activated catalyst to obtain a first mixed carbon-fixing raw material, wherein the mixing mass of the desulfurized gypsum is 8% of the mass of the slag steel, and the Na is 2 SiO 3 The mixing mass is 8% of the slag steel mass, and the ratio of the liquid activation catalyst mixing mass to the solid raw material mass is 1:1, wherein the solid raw materials comprise the slag steel, desulfurized gypsum and Na 2 SiO 3 The liquid activated catalyst comprises acetic acid and water, and the volume ratio of the acetic acid to the water is 1:30.in the present embodiment, in Na 2 SiO 3 Under the combined mixed excitation action with the desulfurized gypsum, the glassy Si-O bond and A1-O bond in the steel slag are destroyed, so that the glass body is rapidly dissociated, a large number of silica ion groups and alumina ion groups are generated, and the silica ion groups and the alumina ion groups are combined with Ca in the liquid phase of the steel slag 2+ 、A1 3+ Plasma reaction to produce large amounts of hydrated calcium aluminate, hydrated calcium silicate and hydrated calcium sulfoaluminate, which are fed to the first carbon-fixing reactor and then reacted with CO 2 The contact is easy to carbonize and generate calcium carbonate, the carbon fixing capability of the steel slag is improved, and simultaneously, caO and MgO in the steel slag meet H under the action of a liquid active catalyst in the mixing process of a vertical mixer 2 Conversion of O to Ca (OH) 2 、Mg(OH) 2 Enters a first carbon-fixing reactor and then is reacted with CO 2 And calcium carbonate and magnesium carbonate are formed by reaction, so that the carbon fixing capability of the steel slag is improved.|[0040] S2, introducing the mixed carbon-fixing raw material into a first reaction bin, and enabling the mixed carbon-fixing raw material to pass through a material conveyor, a plurality of airflow amplifiers and CO to be absorbed at a first processing temperature 2 And (3) reacting to obtain a second mixed carbon-fixing raw material after primary carbon fixing. Further, the first processing temperature is 60 ℃.|[0041] S3, crushing the second mixed carbon-fixing raw material, introducing the crushed second mixed carbon-fixing raw material into a second carbon-fixing reaction mechanism, spraying NaOH into the second carbon-fixing reaction mechanism, and providing CO to be absorbed to the second carbon-fixing reaction mechanism from the lateral direction and the bottom through a first air inlet component and a second air inlet component respectively 2 The second mixed carbon-fixing raw material, the NaOH and the CO to be absorbed are in a suspension fluidization state 2 Reacting to obtain a third mixed carbon-fixing raw material; further, in the step S3, the concentration of NaOH is 1.8%, and the ratio of the mass of the NaOH solution to the mass of the solid raw material is 4%; the air supply amount of the first air inlet component is 0.1m 3 /h; the air supply amount of the second air inlet component is 2.0m 3 And/h. In this embodiment, CO in the tail gas of the cement decomposing kiln is introduced 2 Absorbed by NaOH to form Na 2 CO 3 The unreacted carbon-fixing raw material entering the second carbon-fixing reactor is leached out to form Ca (OH) by the action of NaOH 2 、Mg(OH) 2 After that, na 2 CO 3 Respectively with Ca (OH) 2 、Mg(OH) 2 Reacting to generate CaCO 3 And MgCO 3 And (5) carbon fixation products. Meanwhile, the shaking assembly synchronously works to ensure that the process is smoothly carried out.|[0042] S4, recycling the third mixed carbon-fixing raw material. Further, the step S4 specifically includes: separating gaseous matters and solid matters from the third mixed carbon-fixing raw material after cyclone dust removal and cloth bag dust removal in sequence, and introducing the gaseous matters into a chimney to recycle the solid matters. Specifically, in the embodiment, the smoke emission concentration after bag dust removal is less than or equal to 10mg/m 3 The solid carbon steel slag micropowder in the solid matters after the reaction treatment does not have the problem of stability of steel slag, has high activity and high grindability, can be used as a novel carbon-fixing high-quality mixed material for cement production, can be used for preparing a carbon-fixing high-efficiency composite admixture by synergism of other low-price industrial solid wastes, can also replace mineral powder in cement production and reduce clinker consumption, and can also replace mineral powder in concrete production, improve concrete performance quality and reduce cement consumption.|[0043] Example III|[0044] The embodiment provides another two-stage carbon fixing method for industrial solid waste, which is implemented by adopting the two-stage carbon fixing device for industrial solid waste described in the first embodiment, and specifically comprises the following steps:|[0045] s1, mixing slag steel, desulfurized gypsum and Na in a mixing mechanism 2 SiO 3 And a liquid activated catalyst to obtain a first mixed carbon-fixing raw material, wherein the mixing mass of the desulfurized gypsum is 10% of the mass of the slag steel, and the Na is 2 SiO 3 The mixing mass is 10% of the slag steel mass, and the ratio of the liquid activation catalyst mixing mass to the solid raw material mass is 3:1, wherein the solid raw materials comprise the slag steel, desulfurized gypsum and Na 2 SiO 3 The liquid activated catalyst comprises acetic acid and water, and the volume ratio of the acetic acid to the water is 1:50. in the present embodiment, in Na 2 SiO 3 Under the combined mixed excitation action with the desulfurized gypsum, the glassy Si-O bond and the A1-O bond in the steel slag are destroyed, so that the glass body is quickly brokenRapidly dissociates and generates a large amount of silicon oxygen ion groups and aluminum oxygen ion groups, which are matched with Ca in the liquid phase of steel slag 2+ 、A1 3+ Plasma reaction to produce large amounts of hydrated calcium aluminate, hydrated calcium silicate and hydrated calcium sulfoaluminate, which are fed to the first carbon-fixing reactor and then reacted with CO 2 The contact is easy to carbonize and generate calcium carbonate, the carbon fixing capability of the steel slag is improved, and simultaneously, caO and MgO in the steel slag meet H under the action of a liquid active catalyst in the mixing process of a vertical mixer 2 Conversion of O to Ca (OH) 2 、Mg(OH) 2 Enters a first carbon-fixing reactor and then is reacted with CO 2 And calcium carbonate and magnesium carbonate are formed by reaction, so that the carbon fixing capability of the steel slag is improved.|[0046] S2, introducing the mixed carbon-fixing raw material into a first reaction bin, and enabling the mixed carbon-fixing raw material to pass through a material conveyor, a plurality of airflow amplifiers and CO to be absorbed at a first processing temperature 2 And (3) reacting to obtain a second mixed carbon-fixing raw material after primary carbon fixing. Further, the first processing temperature is 80 ℃.|[0047] S3, crushing the second mixed carbon-fixing raw material, introducing the crushed second mixed carbon-fixing raw material into a second carbon-fixing reaction mechanism, spraying NaOH into the second carbon-fixing reaction mechanism, and providing CO to be absorbed to the second carbon-fixing reaction mechanism from the lateral direction and the bottom through a first air inlet component and a second air inlet component respectively 2 The second mixed carbon-fixing raw material, the NaOH and the CO to be absorbed are in a suspension fluidization state 2 Reacting to obtain a third mixed carbon-fixing raw material; further, in the step S3, the concentration of NaOH is 2.2%, and the ratio of the mass of the NaOH solution to the mass of the solid raw material is 8%; the air supply amount of the first air inlet component is 0.3m 3 /h; the air supply amount of the second air inlet component is 3.0m 3 And/h. In this embodiment, CO in the tail gas of the cement decomposing kiln is introduced 2 Absorbed by NaOH to form Na 2 CO 3 The unreacted carbon-fixing raw material entering the second carbon-fixing reactor is leached out to form Ca (OH) by the action of NaOH 2 、Mg(OH) 2 After that, na 2 CO 3 Respectively with Ca (OH) 2 、Mg(OH) 2 Reacting to generate CaCO 3 And MgCO 3 And (5) carbon fixation products. At the same time, the wobble assembly is synchronizedAnd (3) operating to ensure that the process is smoothly performed.|[0048] S4, recycling the third mixed carbon-fixing raw material. Further, step S4 specifically includes: separating gaseous matters and solid matters from the third mixed carbon-fixing raw material after cyclone dust removal and cloth bag dust removal in sequence, and introducing the gaseous matters into a chimney to recycle the solid matters. Specifically, in the embodiment, the smoke emission concentration after bag dust removal is less than or equal to 10mg/m 3 The solid carbon steel slag micropowder in the solid matters after the reaction treatment does not have the problem of stability of steel slag, has high activity and high grindability, can be used as a novel carbon-fixing high-quality mixed material for cement production, can be used for preparing a carbon-fixing high-efficiency composite admixture by synergism of other low-price industrial solid wastes, can also replace mineral powder in cement production and reduce clinker consumption, and can also replace mineral powder in concrete production, improve concrete performance quality and reduce cement consumption.|[0049] Example IV|[0050] The present embodiment provides another two-stage carbon sequestration method for industrial waste solids, which is implemented using the two-stage carbon sequestration device for industrial waste solids described in embodiment one. In the embodiment, steel slag powder after steel slag powder grinding treatment by adopting a steel group converter heat-stewed steel slag powder grinding treatment is adopted, the grain size of micro powder is 200-250 meshes, and chemical components (mass ratio%) are shown in table 1:|[0051] TABLE 1 chemical composition of steel slag in example IV|[0052] Alkalinity (basicity)CaOSiO 2Al 2 O 3Fe 2 O 3MgOP 2 O 5MnO2.4142.8317.2010.7916.485.611.932.75|[0053] The invention adopts the desulfurization gypsum from the limestone-gypsum wet flue gas desulfurization process of the power plant, which mainly contains 31.55 percent of CaO, 2.07 percent of SiO and 66.38 percent of other components. Further, in this example, the amount of the desulfurized gypsum to be added was 1t/d, na 2 SiO 3 The doping amount is 0.6t/d, and the volume ratio of acetic acid to water is 1:40 to prepare the liquid activated catalyst, wherein the mixing amount of the liquid activated catalyst in the vertical mixer is 15t/d.|[0054] In this embodiment, the gas flow amplifier channels the cement kiln exhaust gas filled in the two-stage carbon sequestration plant to the first carbon sequestration reactor by consuming a small portion of the compressed air, so that the flue gas concentration in the first carbon sequestration reactor increases (CO 2 Concentration about 37-40%). And finally, the carbon-fixing product enters a finished product warehouse. The tail gas of the cement decomposing kiln after the carbon fixation reaction enters a cyclone dust collector, and the smoke dust emission concentration is less than or equal to 10mg/m after cyclone dust collection and cloth bag dust collection 3 And (3) entering a chimney, cyclone dust removal and carbon fixation products collected at the lower end of a bag-type dust remover, and entering a finished product warehouse.|[0055] Comparative example one|[0056] In the comparative example, acetic acid and Na are added into a mixing mechanism 2 SiO 3 And water (without adding desulfurization gypsum from the limestone-gypsum wet flue gas desulfurization process of the power plant), other components and processing modes are the same as in the fourth embodiment.|[0057] Comparative example two|[0058] In this comparative example, desulfurized gypsum, acetic acid and water (no Na was added) were added to a mixing mechanism 2 SiO 3 ) Other components and processing methods were the same as in example four.|[0059] The carbon content (mass percent%) of the carbon-fixing raw materials and the carbon-fixing products in the fourth example, the first comparative example and the second comparative example are respectively measured by a American LECO CS-344 carbon-sulfur analyzer, and then the carbon-fixing rate (%) of the carbon-fixing raw materials is calculated by adopting the following formula:|[0060] |[0061] in the above formula, m1 and m0 respectively represent the mass of the carbon-fixing product and the mass of the carbon-fixing raw material, and c1 and c0 respectively represent the carbon content (mass percent) of the carbon-fixing product and the carbon-fixing raw material. The average carbon fixation rate obtained by the calculation of the systems of the fourth embodiment, the first comparative embodiment and the second comparative embodiment after continuous operation for one month is shown in fig. 6, and as can be seen from fig. 6, the average carbon fixation rate of the fourth embodiment is obviously higher, so that the method provided by the application has better carbon fixation effect.|[0062] In summary, the industrial solid waste two-stage carbon fixing device and method of the invention performs physical adsorption and chemical absorption on the tail gas of the cement decomposing kiln through the first carbon fixing reaction mechanism 200 and the second carbon fixing reaction mechanism 400, and can perform physical adsorption and chemical absorption on CO in the tail gas of the cement decomposing kiln 2 On one hand, the method has the remarkable advantages of high matching degree, good carbon fixing effect, high automation degree and the like in the whole carbon fixing process through reasonable structural layout and internal creative carbon fixing mechanism setting, on the other hand, the steel slag micro powder after carbon fixing has no stability problem, has higher activity and wear resistance, can be used as a novel carbon fixing high-quality mixed material for cement production,the method can also be used for preparing the carbon-fixing high-efficiency composite admixture by the synergism of other low-price industrial solid wastes, thereby being capable of replacing mineral powder and reducing the clinker consumption in cement production, and simultaneously, the steel slag micro powder after carbon fixing can also be used for replacing mineral powder in concrete production, thereby improving the performance and quality of concrete and reducing the cement consumption. Therefore, the method has excellent practical use value, and is a novel industrial solid waste two-stage carbon fixing device and method with wide use prospect.|[0063] It is apparent that the above examples are given by way of illustration only and are not limiting of the embodiments. Other variations and modifications of the present invention will be apparent to those of ordinary skill in the art in light of the foregoing description. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present invention. (CN117861518)|TECHNICAL FIELD|[0001] The invention relates to the field of carbon dioxide emission reduction treatment, in particular to an industrial solid waste two-stage carbon fixing device and method.|BACKGROUND ART|[0002] The cement industry occupies a significant proportion of the global anthropogenic carbon dioxide emissions, about 7% of the global anthropogenic carbon dioxide emissions, and about 12% of the global industrial emissions. According to the 2DS convention of paris protocol in 2015, the global cement industry was required to achieve the goal of carbon neutralization in 2050 and a 40% reduction in carbon was necessary in 2030. The cement yield in 2022 in China is about 21.18 hundred million tons, and if calculated by about 604.7kg of carbon emission per ton of cement counted by China cement institute, the carbon dioxide emitted by the cement industry is about 12.8 hundred million tons. Facing such tremendous carbon emission reduction tasks, the cement industry needs to find new emission reduction routes.|[0003] The carbon dioxide gas generated by the cement industry is converted into carbonate or a new carbon-containing product, and a new direction is provided for carbon emission reduction of the cement industry. Particularly, the industries capable of consuming a large amount of carbon dioxide become support industries for realizing large-scale carbon emission reduction in the cement industry.|[0004] Steel slag is a solid waste produced in the steelmaking process, and the yield of the steel slag is about 15-20% of the yield of coarse steel. However, the actual utilization rate of the steel slag in China is only 30%, a large amount of steel slag is abandoned and piled up, and a large amount of land is occupied. The steel slag contains hydraulic material, and can be used as cementing material to replace silicate cement clinker after being ground. However, steel slag and tailings after treatment thereof have difficulty in large-scale building material utilization. The main reason is that the activity of the steel slag in cement and concrete building materials is low, and the steel slag contains a large amount of free oxides, and the free oxides are easy to expand in volume when meeting water, so that micro cracks appear in the building materials, and the strength is further reduced.|[0005] A large amount of calcium magnesium oxide in the steel slag can be used for capturing CO 2 The higher reactivity and the inherent alkalinity of the carrier make it more suitable for mineralizing CO 2 Mineralizing and sealing CO by utilizing steel slag 2 Not only can lighten CO 2 The discharge pressure of the steel slag can also improve the recycling utilization rate of the steel slag, and the mineralized steel slag has stable structure and can be better applied to the fields of building materials, roadbed materials and the like, so how to recycle the steel slag and combine the steel slag with a carbon fixation technology is a great direction of the development of the industry.|DISCLOSURE|Disclosure of Invention|[0006] Therefore, the invention aims to solve the technical problem of using steel slag in the carbon fixing technology in the prior art and provides an industrial solid waste two-stage carbon fixing device and method.|[0007] In order to solve the technical problems, the invention provides an industrial solid waste two-stage carbon fixing device, which comprises: a mixing mechanism; a first carbon sequestration reaction mechanism comprising: the material conveying device comprises a first reaction bin, a material conveyor and a plurality of air flow amplifiers, wherein the first reaction bin is communicated with the mixing mechanism, the material conveyor is arranged inside the first reaction bin, and the air flow amplifiers are communicated with the first reaction bin; the communicating mechanism comprises a communicating pipe and a crusher, one end of the communicating pipe is communicated with the first reaction bin, and the crusher is arranged inside the communicating pipe; a second carbon sequestration reaction mechanism comprising: the device comprises a second reaction bin, a first air inlet component, a second air inlet component and a plurality of spray guns, wherein the second reaction bin is communicated with the other end of the communicating pipe, the spray guns, the first air inlet component and the second air inlet component are all communicated with the second reaction bin, the first air inlet component faces to the outlet of the second reaction bin, and the second air inlet component is arranged at the bottom of the second reaction bin.|[0008] In one embodiment of the invention, the first carbon-fixing reaction mechanism further comprises a temperature control component, and the temperature control component is connected with the first reaction bin.|[0009] In one embodiment of the invention, the mixing mechanism comprises a mixing bin and a first discharge valve, wherein the mixing bin is communicated with the first reaction bin, the first discharge valve is arranged at the discharge end of the mixing bin, and the communication mechanism further comprises a second discharge valve which is arranged at the discharge end of the communication pipe.|[0010] In an embodiment of the invention, the second carbon-fixing reaction mechanism further comprises a reaction bed and a third discharge valve, and the first air inlet component and the third discharge valve are respectively arranged at two ends of the reaction bed.|[0011] In one embodiment of the invention, the first air intake assembly comprises a first air intake pipe; the second air inlet assembly comprises a plurality of second air inlet pipes and a plurality of adjusting air valves, wherein the second air inlet pipes correspond to each other one by one.|[0012] In one embodiment of the invention, the device further comprises an auxiliary mechanism, wherein the auxiliary mechanism comprises a base and at least one shaking assembly, at least one shaking assembly is arranged on the base and comprises a bearing seat, a speed reducer, a linkage assembly and an eccentric shaft, the bearing seat supports the second carbon fixation reaction mechanism, one end of the eccentric shaft is connected with the bearing support seat, the other end of the eccentric shaft is connected with the linkage assembly, and the linkage assembly is connected with the speed reducer.|[0013] The invention also provides an industrial solid waste two-stage carbon fixing method which is implemented by adopting the industrial solid waste two-stage carbon fixing device,the method specifically comprises the following steps: s1, mixing slag steel, desulfurized gypsum and Na in a mixing mechanism 2 SiO 3 And activating the catalyst in a liquid state to obtain a first mixed carbon-fixing raw material; s2, introducing the mixed carbon-fixing raw material into a first reaction bin, and enabling the mixed carbon-fixing raw material to pass through a material conveyor, a plurality of airflow amplifiers and CO to be absorbed at a first processing temperature 2 Obtaining a second mixed carbon-fixing raw material after primary carbon fixing; s3, crushing the second mixed carbon-fixing raw material, introducing the crushed second mixed carbon-fixing raw material into a second carbon-fixing reaction mechanism, spraying NaOH into the second carbon-fixing reaction mechanism, and providing CO to be absorbed to the second carbon-fixing reaction mechanism from the lateral direction and the bottom through a first air inlet component and a second air inlet component respectively 2 The second mixed carbon-fixing raw material, the NaOH and the CO to be absorbed are in a suspension fluidization state 2 Reacting to obtain a third mixed carbon-fixing raw material; s4, recycling the third mixed carbon-fixing raw material.|[0014] In one embodiment of the present invention, the desulphurized gypsum in the step S1 is doped with 8-10% of the slag steel mass, and the Na is 2 SiO 3 The doping mass is 8% -10% of the slag steel mass, and the ratio of the liquid activation catalyst doping mass to the solid raw material mass is 1:1 to 3:1, wherein the solid raw materials comprise the slag steel, desulfurized gypsum and Na 2 SiO 3 The liquid activated catalyst comprises acetic acid and water, and the volume ratio of the acetic acid to the water is 1: 30-1: 50.|[0015] in one embodiment of the present invention, in step S2, the first processing temperature is 60 to 80 ℃; in the step S3, the concentration of NaOH is 1.8-2.2%, and the ratio of the mass of the NaOH solution to the mass of the solid raw material is 4% -8%; the air supply amount of the first air inlet component is 0.1-0.3 m 3 /h; the air supply amount of the second air inlet component is 2.0-3.0 m 3 /h。|[0016] In one embodiment of the present invention, step S4 specifically includes: separating gaseous matters and solid matters from the third mixed carbon-fixing raw material after cyclone dust removal and cloth bag dust removal in sequence, and introducing the gaseous matters into a chimney to recycle the solid matters.|[0017] Compared with the prior art, the technical scheme of the invention has the following advantages:|[0018] according to the industrial solid waste two-stage carbon fixing device and method, the first carbon fixing reaction mechanism and the second carbon fixing reaction mechanism are used for carrying out physical adsorption and chemical absorption on the tail gas of the cement decomposing kiln, so that CO in the tail gas of the cement decomposing kiln can be absorbed 2 On the one hand, the carbon fixing device is arranged through reasonable structural layout and an internal creative carbon fixing mechanism, so that the whole carbon fixing process has the remarkable advantages of high matching degree, good carbon fixing effect, high automation degree and the like, on the other hand, the carbon fixing slag micro powder after carbon fixing has no stability problem of steel slag, has higher activity and wear resistance, can be used as a novel carbon fixing high-quality mixed material for cement production, and can also be used for preparing high-efficiency carbon fixing composite admixture by synergic preparation of other low-price industrial solid wastes, thereby being capable of replacing mineral powder and reducing clinker consumption in cement production, further replacing mineral powder in concrete production, improving concrete performance quality and reducing cement consumption. Therefore, the method has excellent practical use value, and is a novel industrial solid waste two-stage carbon fixing device and method with wide use prospect.|DRAWINGS DESCRIPTION|[0019] In order that the invention may be more readily understood, a more particular description of the invention will be rendered by reference to specific embodiments thereof that are illustrated in the appended drawings.|[0020] FIG. 1 is a schematic perspective view of an industrial solid waste two-stage carbon fixing device in a preferred embodiment of the invention;|[0021] FIG. 2 is a side view of the industrial waste two-stage carbon fixing device of FIG. 1;|[0022] FIG. 3 is a schematic cross-sectional view taken at A-A of FIG. 2;|[0023] FIG. 4 is a top view of the reaction bed of FIG. 1;|[0024] FIG. 5 is a schematic view of the auxiliary mechanism of FIG. 1;|[0025] FIG. 6 is a bar chart showing the average carbon fixation in the fourth, first and second examples of the present invention.|[0026] Description of the specification reference numerals: 100. a mixing mechanism; 110. a mixing bin; 120. a first discharge valve; 200. a first carbon sequestration reaction mechanism; 210. a first reaction bin; 220. a material conveyor; 230. an air flow amplifier; 300. a communication mechanism; 310. a communicating pipe; 320. a crusher; 330. a second discharge valve; 400. a second carbon fixing mechanism; 410. a second reaction bin; 411. a third discharge valve; 412. a reaction bed; 420. a first air intake assembly; 421. a first air inlet pipe; 430. a second air intake assembly; 431. a second air inlet pipe; 432. adjusting an air valve; 440. a spray gun; 450. a vibration hammer; 500. an auxiliary mechanism; 510. a base; 520. shaking the assembly; 530. a bearing seat; 540. a speed reducer; 550. an eccentric shaft; 560. and a linkage assembly.|INVENTION MODE|Detailed Description|[0027] The present invention will be further described with reference to the accompanying drawings and specific examples, which are not intended to be limiting, so that those skilled in the art will better understand the invention and practice it.|[0028] Example 1|[0029] Referring to fig. 1 to 3, the present embodiment provides an industrial solid waste two-stage carbon fixing device, which includes: a mixing mechanism 100; a first carbon sequestration reaction mechanism 200 comprising: the material mixing device comprises a first reaction bin 210, a material conveyor 220 and a plurality of air flow amplifiers 230, wherein the first reaction bin 210 is communicated with the material mixing mechanism 100, the material conveyor 220 is arranged inside the first reaction bin 210, and the air flow amplifiers 230 are communicated with the first reaction bin 210; a communicating mechanism 300 including a communicating pipe 310 and a crusher 320, wherein one end of the communicating pipe 310 communicates with the first reaction chamber 210, and the crusher 320 is disposed inside the communicating pipe 310; a second carbon sequestration reaction mechanism 400 comprising: the second reaction bin 410, the first air inlet assembly 420, the second air inlet assembly 430 and the plurality of spray guns 440, wherein the second reaction bin 410 is communicated with the other end of the communicating pipe 310, the plurality of spray guns 440, the first air inlet assembly 420 and the second air inlet assembly 430 are all communicated with the second reaction bin 410, the first air inlet assembly 420 faces to the outlet of the second reaction bin 410, and the second air inlet assembly 430 is arranged at the bottom of the second reaction bin 410.|[0030] The industrial solid waste two-stageThe carbon fixing device performs physical adsorption and chemical absorption on the tail gas of the cement decomposing kiln through the first carbon fixing reaction mechanism 200 and the second carbon fixing reaction mechanism 400, and can perform physical adsorption and chemical absorption on CO in the tail gas of the cement decomposing kiln 2 On one hand, the method has the remarkable advantages of high cooperation degree, good carbon fixing effect, high automation degree and the like in the whole carbon fixing process, and on the other hand, the steel slag micro powder after carbon fixing has no stability problem, has higher activity and wear resistance, can be used as a novel carbon fixing high-quality mixed material for cement production, and can also be used as a novel carbon fixing high-efficiency composite admixture for preparing other low-price industrial solid wastes in a synergistic manner, thereby being capable of replacing mineral powder and reducing clinker consumption in cement production, and simultaneously, the steel slag micro powder after carbon fixing can also replace mineral powder in concrete production, improve concrete performance quality and reduce cement consumption. Therefore, the method has excellent practical use value, and is a novel industrial solid waste two-stage carbon fixing device with wide use prospect.|[0031] Referring to fig. 1 to 3, in this embodiment, in the height direction of the apparatus, a mixing mechanism 100, a first carbon fixing reaction mechanism 200, a communication mechanism 300 and a second carbon fixing reaction mechanism 400 are sequentially connected from top to bottom, where the mixing mechanism 100 is used to mix steel slag powder after grinding of thermally braised steel slag in a converter and desulfurized gypsum (the main component is CaSO 4 ·2H 2 O) to produce a mixture capable of mixing with CO in the tail gas of a cement-decomposing kiln 2 Fully reacted carbon-fixing raw material, the first carbon-fixing reaction mechanism 200 is used for CO 2 The first carbon fixation process is performed, the communication mechanism 300 is used for crushing the solid raw material carrying a large amount of steel slag after the first reaction, so that the solid raw material can smoothly enter the second carbon fixation reaction mechanism 400 for operation, and the second carbon fixation reaction mechanism 400 is used for mixing the crushed powder raw material with an alkaline solution such as strong sodium oxide and the like to realize CO 2 Thereby achieving the purpose of fully fixing carbon. The used carbon-fixing product can be used as a mixture to produce low-carbon cement or used as a concrete admixture, therebyRealizing the comprehensive utilization of wastes.|[0032] Referring to fig. 3, the mixing mechanism 100 includes a mixing bin 110 and a first discharge valve 120, where the mixing bin 110 is communicated with the first reaction bin 210, and the first discharge valve 120 is disposed at a discharge end of the mixing bin 110. In this embodiment, the first discharge valve 120 is used to control the discharge amount and the discharge speed in the mixing bin 110. Further, a stirring device is provided in the mixing bin 110.|[0033] Referring to fig. 3, the first carbon-fixing reaction mechanism 200 further includes a housing, and the first reaction chamber 210 is preferably a reaction pipe provided inside the housing, and the housing communicates with the second carbon-fixing reaction mechanism 400, thereby filling the periphery of the first reaction chamber 210 with CO to be absorbed 2 In the first carbon sequestration reaction mechanism 200, the CO to be absorbed 2 The gas flow amplifiers 230 enter the first reaction chamber 210, and further, the gas flow amplifiers 230 are uniformly spaced along the extending direction of the first reaction chamber 210, and the gas flow amplifiers 230 consume a small amount of compressed air to fill the CO to be absorbed outside the first reaction chamber 210 2 The flue gas is guided into the first reaction chamber 210, so that the flue gas concentration of the first reaction chamber 210 is increased, the temperature in the first reaction chamber 210 is increased under the action of the air flow amplifier 230, and at the same time, the carbon-fixing raw material slowly moves forward under the conveying action of the material conveyor 220, thereby absorbing CO 2 Fully react to realize CO in the flue gas 2 Is a primary emission reduction of the fuel. Further, in this embodiment, the first carbon-fixing reaction mechanism 200 further includes a temperature control component, and the temperature control component is connected to the first reaction chamber 210, and further, the material conveyor 220 in this embodiment is preferably a screw conveyor. In addition, in this embodiment, the average temperature range in the first carbon fixing reaction mechanism 200 is kept at 60-80 ℃, and this temperature range can promote the carbon fixing reaction of the carbon fixing raw material, accelerate the carbon fixing reaction process, and improve the carbon fixing efficiency. In particular, the present invention is not limited to the specific kind of temperature control assembly.|[0034] In this embodiment, the communication mechanism 300 further includes a second discharge valve 330, where the second discharge valve 330 is disposed at a discharge end of the communication pipe 310. Further, the second discharge valve 330 in this embodiment can control the discharge amount and the discharge speed of the communication mechanism 300, the carbon-fixing product and the unreacted carbon-fixing raw material discharged from the first carbon-fixing reaction mechanism 200 enter the crusher 320 through the communication pipe 310, and are ground into powder under the action of the crusher 320, the particle size of the micro powder required in this embodiment is about 250-280 mesh, and the micro powder of the ground carbon-fixing product and the unreacted carbon-fixing raw material enter the second carbon-fixing reaction mechanism 400 through the discharge valve.|[0035] Referring to fig. 3 and 4, the second carbon-fixing reaction mechanism 400 further includes a reaction bed 412 and a third discharge valve 411, wherein the first air inlet assembly 420 and the third discharge valve 411 are respectively disposed at two ends of the reaction bed 412, and specifically, the first air inlet assembly 420 includes a first air inlet pipe 421; the second air intake assembly 430 includes a plurality of second air intake pipes 431 and a plurality of air regulating valves 432 in a one-to-one correspondence. In this embodiment, the material entering the second carbon-fixing reaction mechanism 400 through the communication mechanism 300 moves towards the third discharge valve 411 under the action of the first air inlet component 420, and at the same time, the carbon-fixing raw material micropowder forms suspension fluidization under the action of the second air inlet component 430, so that on one hand, the movement process of the material can be smoother, the material is prevented from adhering to the surface of the reaction bed 412, and on the other hand, the arrangement can enlarge the material and the CO to be absorbed 2 Further improving the carbon fixation effect of absorption. Specifically, in the present embodiment, the air volume of the first air intake assembly 420 is set to be 0.1-0.3 m 3 And/h, the air volume of the second air inlet assembly 430 is set to be 2.0-3.0 m 3 And/h. In this embodiment, the plurality of spray guns 440 are uniformly spaced along the moving direction of the material and are used for spraying NaOH solution into the second reaction chamber 410, wherein the NaOH solution is used for mixing with the material and the CO to be absorbed 2 The second air inlet pipes 431 can be independently adjusted through the adjusting air valves 432 to improve the flexibility of the equipment. In addition, in the present embodiment, a plurality of hammers 450 are further provided on the sidewall of the second reaction chamber 410 to prevent powder from being deposited in the second carbon-fixing reactor.|[0036] Referring to fig. 5, the auxiliary mechanism 500 further includes an auxiliary mechanism 500, where the auxiliary mechanism 500 includes a base 510 and at least one shaking assembly 520, at least one shaking assembly 520 is disposed on the base 510, and includes a bearing seat 530, a speed reducer 540, a linkage assembly 560, and an eccentric shaft 550, where the bearing seat 530 supports the second carbon-fixing reaction mechanism 400, one end of the eccentric shaft 550 is connected to the bearing support, the other end is connected to the linkage assembly 560, and the linkage assembly 560 is connected to the speed reducer 540. The auxiliary mechanism 500 in this embodiment includes two shaking assemblies 520 disposed at two ends of the base 510 along the length direction thereof, the shaking assemblies 520 enable shaking of a certain frequency to occur during the operation of the first carbon fixing reaction mechanism 200 and the second carbon fixing reaction mechanism 400, and by continuously shaking, the adhesion of carbon fixing products or unreacted carbon fixing raw materials to the inner surface of the first reaction chamber 210 or the second reaction chamber 410 is prevented, meanwhile, the probability of agglomeration of the materials on the reaction bed 412 is greatly reduced by the shaking assemblies 520, and the shaking assemblies 520 can continuously strip the reactants, impurities and surface passivation layers deposited by adsorption on the solid surface to expose new active surfaces, thereby enhancing the internal diffusion mass transfer rate, continuously shrinking solid particles, increasing the effective contact area of gas and solid, and improving the carbon fixing efficiency of the carbon fixing raw materials. Further, in the auxiliary mechanism 500 of the present embodiment, the eccentric amount of the shaking unit 520 is 12 to 15mm and the rotational speed is 20 to 40 rpm.|[0037] Example two|[0038] The embodiment provides an industrial solid waste two-stage carbon fixing method, which is implemented by adopting the industrial solid waste two-stage carbon fixing device in the first embodiment, and specifically comprises the following steps:|[0039] s1, mixing slag steel, desulfurized gypsum and Na in a mixing mechanism 2 SiO 3 And a liquid activated catalyst to obtain a first mixed carbon-fixing raw material, wherein the mixing mass of the desulfurized gypsum is 8% of the mass of the slag steel, and the Na is 2 SiO 3 The mixing mass is 8% of the slag steel mass, and the ratio of the liquid activation catalyst mixing mass to the solid raw material mass is 1:1, wherein the solid raw materials comprise the slag steel, desulfurized gypsum and Na 2 SiO 3 The liquid activated catalyst comprises acetic acid and water, and the volume ratio of the acetic acid to the water is 1:30.in the present embodiment, in Na 2 SiO 3 Under the combined mixed excitation action with the desulfurized gypsum, the glassy Si-O bond and A1-O bond in the steel slag are destroyed, so that the glass body is rapidly dissociated, a large number of silica ion groups and alumina ion groups are generated, and the silica ion groups and the alumina ion groups are combined with Ca in the liquid phase of the steel slag 2+ 、A1 3+ Plasma reaction to produce large amounts of hydrated calcium aluminate, hydrated calcium silicate and hydrated calcium sulfoaluminate, which are fed to the first carbon-fixing reactor and then reacted with CO 2 The contact is easy to carbonize and generate calcium carbonate, the carbon fixing capability of the steel slag is improved, and simultaneously, caO and MgO in the steel slag meet H under the action of a liquid active catalyst in the mixing process of a vertical mixer 2 Conversion of O to Ca (OH) 2 、Mg(OH) 2 Enters a first carbon-fixing reactor and then is reacted with CO 2 And calcium carbonate and magnesium carbonate are formed by reaction, so that the carbon fixing capability of the steel slag is improved.|[0040] S2, introducing the mixed carbon-fixing raw material into a first reaction bin, and enabling the mixed carbon-fixing raw material to pass through a material conveyor, a plurality of airflow amplifiers and CO to be absorbed at a first processing temperature 2 And (3) reacting to obtain a second mixed carbon-fixing raw material after primary carbon fixing. Further, the first processing temperature is 60 ℃.|[0041] S3, crushing the second mixed carbon-fixing raw material, introducing the crushed second mixed carbon-fixing raw material into a second carbon-fixing reaction mechanism, spraying NaOH into the second carbon-fixing reaction mechanism, and providing CO to be absorbed to the second carbon-fixing reaction mechanism from the lateral direction and the bottom through a first air inlet component and a second air inlet component respectively 2 The second mixed carbon-fixing raw material, the NaOH and the CO to be absorbed are in a suspension fluidization state 2 Reacting to obtain a third mixed carbon-fixing raw material; further, in the step S3, the concentration of NaOH is 1.8%, and the ratio of the mass of the NaOH solution to the mass of the solid raw material is 4%; the air supply amount of the first air inlet component is 0.1m 3 /h; the air supply amount of the second air inlet component is 2.0m 3 And/h. In this embodiment, CO in the tail gas of the cement decomposing kiln is introduced 2 Absorbed by NaOH to form Na 2 CO 3 The unreacted carbon-fixing raw material entering the second carbon-fixing reactor is leached out to form Ca (OH) by the action of NaOH 2 、Mg(OH) 2 After that, na 2 CO 3 Respectively with Ca (OH) 2 、Mg(OH) 2 Reacting to generate CaCO 3 And MgCO 3 And (5) carbon fixation products. Meanwhile, the shaking assembly synchronously works to ensure that the process is smoothly carried out.|[0042] S4, recycling the third mixed carbon-fixing raw material. Further, the step S4 specifically includes: separating gaseous matters and solid matters from the third mixed carbon-fixing raw material after cyclone dust removal and cloth bag dust removal in sequence, and introducing the gaseous matters into a chimney to recycle the solid matters. Specifically, in the embodiment, the smoke emission concentration after bag dust removal is less than or equal to 10mg/m 3 The solid carbon steel slag micropowder in the solid matters after the reaction treatment does not have the problem of stability of steel slag, has high activity and high grindability, can be used as a novel carbon-fixing high-quality mixed material for cement production, can be used for preparing a carbon-fixing high-efficiency composite admixture by synergism of other low-price industrial solid wastes, can also replace mineral powder in cement production and reduce clinker consumption, and can also replace mineral powder in concrete production, improve concrete performance quality and reduce cement consumption.|[0043] Example III|[0044] The embodiment provides another two-stage carbon fixing method for industrial solid waste, which is implemented by adopting the two-stage carbon fixing device for industrial solid waste described in the first embodiment, and specifically comprises the following steps:|[0045] s1, mixing slag steel, desulfurized gypsum and Na in a mixing mechanism 2 SiO 3 And a liquid activated catalyst to obtain a first mixed carbon-fixing raw material, wherein the mixing mass of the desulfurized gypsum is 10% of the mass of the slag steel, and the Na is 2 SiO 3 The mixing mass is 10% of the slag steel mass, and the ratio of the liquid activation catalyst mixing mass to the solid raw material mass is 3:1, wherein the solid raw materials comprise the slag steel, desulfurized gypsum and Na 2 SiO 3 The liquid activated catalyst comprises acetic acid and water, and the volume ratio of the acetic acid to the water is 1:50. in the present embodiment, in Na 2 SiO 3 Under the combined mixed excitation action with the desulfurized gypsum, the glassy Si-O bond and the A1-O bond in the steel slag are destroyed, so that the glass body is quickly brokenRapidly dissociates and generates a large amount of silicon oxygen ion groups and aluminum oxygen ion groups, which are matched with Ca in the liquid phase of steel slag 2+ 、A1 3+ Plasma reaction to produce large amounts of hydrated calcium aluminate, hydrated calcium silicate and hydrated calcium sulfoaluminate, which are fed to the first carbon-fixing reactor and then reacted with CO 2 The contact is easy to carbonize and generate calcium carbonate, the carbon fixing capability of the steel slag is improved, and simultaneously, caO and MgO in the steel slag meet H under the action of a liquid active catalyst in the mixing process of a vertical mixer 2 Conversion of O to Ca (OH) 2 、Mg(OH) 2 Enters a first carbon-fixing reactor and then is reacted with CO 2 And calcium carbonate and magnesium carbonate are formed by reaction, so that the carbon fixing capability of the steel slag is improved.|[0046] S2, introducing the mixed carbon-fixing raw material into a first reaction bin, and enabling the mixed carbon-fixing raw material to pass through a material conveyor, a plurality of airflow amplifiers and CO to be absorbed at a first processing temperature 2 And (3) reacting to obtain a second mixed carbon-fixing raw material after primary carbon fixing. Further, the first processing temperature is 80 ℃.|[0047] S3, crushing the second mixed carbon-fixing raw material, introducing the crushed second mixed carbon-fixing raw material into a second carbon-fixing reaction mechanism, spraying NaOH into the second carbon-fixing reaction mechanism, and providing CO to be absorbed to the second carbon-fixing reaction mechanism from the lateral direction and the bottom through a first air inlet component and a second air inlet component respectively 2 The second mixed carbon-fixing raw material, the NaOH and the CO to be absorbed are in a suspension fluidization state 2 Reacting to obtain a third mixed carbon-fixing raw material; further, in the step S3, the concentration of NaOH is 2.2%, and the ratio of the mass of the NaOH solution to the mass of the solid raw material is 8%; the air supply amount of the first air inlet component is 0.3m 3 /h; the air supply amount of the second air inlet component is 3.0m 3 And/h. In this embodiment, CO in the tail gas of the cement decomposing kiln is introduced 2 Absorbed by NaOH to form Na 2 CO 3 The unreacted carbon-fixing raw material entering the second carbon-fixing reactor is leached out to form Ca (OH) by the action of NaOH 2 、Mg(OH) 2 After that, na 2 CO 3 Respectively with Ca (OH) 2 、Mg(OH) 2 Reacting to generate CaCO 3 And MgCO 3 And (5) carbon fixation products. At the same time, the wobble assembly is synchronizedAnd (3) operating to ensure that the process is smoothly performed.|[0048] S4, recycling the third mixed carbon-fixing raw material. Further, step S4 specifically includes: separating gaseous matters and solid matters from the third mixed carbon-fixing raw material after cyclone dust removal and cloth bag dust removal in sequence, and introducing the gaseous matters into a chimney to recycle the solid matters. Specifically, in the embodiment, the smoke emission concentration after bag dust removal is less than or equal to 10mg/m 3 The solid carbon steel slag micropowder in the solid matters after the reaction treatment does not have the problem of stability of steel slag, has high activity and high grindability, can be used as a novel carbon-fixing high-quality mixed material for cement production, can be used for preparing a carbon-fixing high-efficiency composite admixture by synergism of other low-price industrial solid wastes, can also replace mineral powder in cement production and reduce clinker consumption, and can also replace mineral powder in concrete production, improve concrete performance quality and reduce cement consumption.|[0049] Example IV|[0050] The present embodiment provides another two-stage carbon sequestration method for industrial waste solids, which is implemented using the two-stage carbon sequestration device for industrial waste solids described in embodiment one. In the embodiment, steel slag powder after steel slag powder grinding treatment by adopting a steel group converter heat-stewed steel slag powder grinding treatment is adopted, the grain size of micro powder is 200-250 meshes, and chemical components (mass ratio%) are shown in table 1:|[0051] TABLE 1 chemical composition of steel slag in example IV|[0052] Alkalinity (basicity)CaOSiO 2Al 2 O 3Fe 2 O 3MgOP 2 O 5MnO2.4142.8317.2010.7916.485.611.932.75|[0053] The invention adopts the desulfurization gypsum from the limestone-gypsum wet flue gas desulfurization process of the power plant, which mainly contains 31.55 percent of CaO, 2.07 percent of SiO and 66.38 percent of other components. Further, in this example, the amount of the desulfurized gypsum to be added was 1t/d, na 2 SiO 3 The doping amount is 0.6t/d, and the volume ratio of acetic acid to water is 1:40 to prepare the liquid activated catalyst, wherein the mixing amount of the liquid activated catalyst in the vertical mixer is 15t/d.|[0054] In this embodiment, the gas flow amplifier channels the cement kiln exhaust gas filled in the two-stage carbon sequestration plant to the first carbon sequestration reactor by consuming a small portion of the compressed air, so that the flue gas concentration in the first carbon sequestration reactor increases (CO 2 Concentration about 37-40%). And finally, the carbon-fixing product enters a finished product warehouse. The tail gas of the cement decomposing kiln after the carbon fixation reaction enters a cyclone dust collector, and the smoke dust emission concentration is less than or equal to 10mg/m after cyclone dust collection and cloth bag dust collection 3 And (3) entering a chimney, cyclone dust removal and carbon fixation products collected at the lower end of a bag-type dust remover, and entering a finished product warehouse.|[0055] Comparative example one|[0056] In the comparative example, acetic acid and Na are added into a mixing mechanism 2 SiO 3 And water (without adding desulfurization gypsum from the limestone-gypsum wet flue gas desulfurization process of the power plant), other components and processing modes are the same as in the fourth embodiment.|[0057] Comparative example two|[0058] In this comparative example, desulfurized gypsum, acetic acid and water (no Na was added) were added to a mixing mechanism 2 SiO 3 ) Other components and processing methods were the same as in example four.|[0059] The carbon content (mass percent%) of the carbon-fixing raw materials and the carbon-fixing products in the fourth example, the first comparative example and the second comparative example are respectively measured by a American LECO CS-344 carbon-sulfur analyzer, and then the carbon-fixing rate (%) of the carbon-fixing raw materials is calculated by adopting the following formula:|[0060] |[0061] in the above formula, m1 and m0 respectively represent the mass of the carbon-fixing product and the mass of the carbon-fixing raw material, and c1 and c0 respectively represent the carbon content (mass percent) of the carbon-fixing product and the carbon-fixing raw material. The average carbon fixation rate obtained by the calculation of the systems of the fourth embodiment, the first comparative embodiment and the second comparative embodiment after continuous operation for one month is shown in fig. 6, and as can be seen from fig. 6, the average carbon fixation rate of the fourth embodiment is obviously higher, so that the method provided by the application has better carbon fixation effect.|[0062] In summary, the industrial solid waste two-stage carbon fixing device and method of the invention performs physical adsorption and chemical absorption on the tail gas of the cement decomposing kiln through the first carbon fixing reaction mechanism 200 and the second carbon fixing reaction mechanism 400, and can perform physical adsorption and chemical absorption on CO in the tail gas of the cement decomposing kiln 2 On one hand, the method has the remarkable advantages of high matching degree, good carbon fixing effect, high automation degree and the like in the whole carbon fixing process through reasonable structural layout and internal creative carbon fixing mechanism setting, on the other hand, the steel slag micro powder after carbon fixing has no stability problem, has higher activity and wear resistance, can be used as a novel carbon fixing high-quality mixed material for cement production,the method can also be used for preparing the carbon-fixing high-efficiency composite admixture by the synergism of other low-price industrial solid wastes, thereby being capable of replacing mineral powder and reducing the clinker consumption in cement production, and simultaneously, the steel slag micro powder after carbon fixing can also be used for replacing mineral powder in concrete production, thereby improving the performance and quality of concrete and reducing the cement consumption. Therefore, the method has excellent practical use value, and is a novel industrial solid waste two-stage carbon fixing device and method with wide use prospect.|[0063] It is apparent that the above examples are given by way of illustration only and are not limiting of the embodiments. Other variations and modifications of the present invention will be apparent to those of ordinary skill in the art in light of the foregoing description. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present invention. Family Number|(109351414)|109351414|Abstract|(CN117861518 A)|The invention provides an industrial solid waste two - stage carbon sequestration device and method . The industrial solid waste two - stage carbon sequestration device comprises a mixing mechanism ; the first carbon sequestration reaction mechanism comprises a first reaction bin , a material conveyor and a plurality of airflow amplifiers ; the communicating mechanism comprises a communicating pipe and a crusher ; and the second carbon sequestration reaction mechanism comprises a second reaction bin , a first gas inlet assembly , a second gas inlet assembly and a plurality of spray guns . The cement decomposition kiln tail gas is subjected to physical adsorption and chemical absorption through the first carbon sequestration reaction mechanism and the second carbon sequestration reaction mechanism , CO2 in the cement decomposition kiln tail gas can be subjected to sufficient carbon sequestration , on one hand , the overall carbon sequestration process has the remarkable advantages of being high in matching degree , good in carbon sequestration effect , high in automation degree and the like , and meanwhile , the carbon sequestration effect is good . The carbon - fixed steel slag micro - powder after carbon fixation does not have the stability problem of steel slag , has higher activity and wear resistance , and can be recycled , so that the carbon - fixed steel slag micro - powder has excellent actual use value and wide use prospect . |CPC codes|(CN117861518 A)|B01D - 053/62 |B01D - 053/75 |B01D - 053/78 |B01D - 053/81 |B01D - 2251/304 |B01D - 2251/402 |B01D - 2251/404 |B01D - 2251/602 |B01D - 2251/604 |B01D - 2257/504 |B01F - 033/83612 |B01F - 033/8362 |IPC codes|(CN117861518 A)|B01D - 053/62 |B01D - 053/75 |B01D - 053/78 |B01D - 053/81 |B01F - 033/80 |B01F - 033/83 |Title|(CN117861518 A)|Industrial solid waste two - stage carbon sequestration device and method | Chemical engineering|Environmental technology|Materials, metallurgy|Other special machines B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/81|B01D-2251/304|B01D-2251/402|B01D-2251/404|B01D-2251/602|B01D-2251/604|B01D-2257/504|B01F-033/83612|B01F-033/8362|B28C-005/00/6|B28C-005/16|C04B-007/153/5|C04B-007/36/7|C04B-007/38|C04B-020/02/3|C04B-020/02/6 (GR1) C04B-020/02/6[RK1]; C04B-020/02/3[RK2]; C04B-018/14/2[RK3] B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/81|B01D-2251/304|B01D-2251/402|B01D-2251/404|B01D-2251/602|B01D-2251/604|B01D-2257/504|B01F-033/83612|B01F-033/8362|B28C-005/00/6|B28C-005/16|C04B-007/153/5|C04B-007/36/7|C04B-007/38|C04B-020/02/3|C04B-020/02/6 B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/81|B01F-033/80|B01F-033/83|B28C-005/00|B28C-005/16|C04B-007/21|C04B-007/36|C04B-007/38|C04B-020/02 B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/81|B01F-033/80|B01F-033/83|B28C-005/00|B28C-005/16|C04B-007/21|C04B-007/36|C04B-007/38|C04B-020/02 PENDING (CN117861518)|PENDING ALIVE (CN117861518)|ALIVE (CN117861518)|LEGAL DETAILS FOR CN117861518|Actual or expected expiration date=2044-01-09|Legal state=ALIVE|Status=PENDING|Event publication date=2024-01-09|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202410031450|Application date=2024-01-09|Standardized application number=2024CN-0031450|Event publication date=2024-04-12|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN117861518|Publication stage code=A|Publication date=2024-04-12|Standardized publication number=CN117861518|Event publication date=2024-04-12|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-04-30|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN117861518)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRM8TPxgfSD2lfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000072245245&ekey=2007&xpn=CN117861518&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=yfJyWjYWnigQAMqbllZa7ZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN117861518)|CN (CN117861518)|NAME=SUZHOU SHIJING TECHNOLOGY CO., LTD. , COUNTRY=CN (CN117861518)|NAME=FENG RUI;CENTRAL SOUTH WELL INTELLECTUAL PROPERTY OFFICE , REG=32257 (CN117861518)|NAME=LU SHOUJIANG|NAME=XIN FENG|NAME=CHENG XINAN|NAME=DONG SHIHONG|NAME=WU QIANQIAN|NAME=HE WEN 0 1 Titre: (CN117861518)|Industrial solid waste two-stage carbon sequestration device and method Résumé: (CN117861518)|The invention provides an industrial solid waste two-stage carbon sequestration device and method. The industrial solid waste two-stage carbon sequestration device comprises a mixing mechanism; the first carbon sequestration reaction mechanism comprises a first reaction bin, a material conveyor and a plurality of airflow amplifiers; the communicating mechanism comprises a communicating pipe and a crusher; and the second carbon sequestration reaction mechanism comprises a second reaction bin, a first gas inlet assembly, a second gas inlet assembly and a plurality of spray guns. The cement decomposition kiln tail gas is subjected to physical adsorption and chemical absorption through the first carbon sequestration reaction mechanism and the second carbon sequestration reaction mechanism, CO2 in the cement decomposition kiln tail gas can be subjected to sufficient carbon sequestration, on one hand, the overall carbon sequestration process has the remarkable advantages of being high in matching degree, good in carbon sequestration effect, high in automation degree and the like, and meanwhile, the carbon sequestration effect is good. The carbon-fixed steel slag micro-powder after carbon fixation does not have the stability problem of steel slag, has higher activity and wear resistance, and can be recycled, so that the carbon-fixed steel slag micro-powder has excellent actual use value and wide use prospect. 18 Abstract gpt-4o-mini no The patent focuses on carbon sequestration from industrial solid waste and involves physical and chemical processes, not on the accelerated weathering of minerals for CO₂ capture.
20 CN202210538978 CN202210538978 CN114680010 100702247 CN114680010 A 2022-07-01 [CN114680010] 2022-05-18 2022-05-18 2022-07-01 (CN114680010)|2042-05-18 (CN114680010)|Sugarcane high-yield planting method giving consideration to soil carbon sequestration and emission reduction in red soil area (CN114680010)|The invention discloses a high-yield sugar cane planting method giving consideration to soil carbon sequestration and emission reduction in a red soil area. The method comprises the following steps: (1) performing crushing, stubble cleaning and linear pre-ditching on previous crop residues by adopting a stubble cleaning and pre-ditching machine; (2) performing soil throwing type deep scarification, deep ploughing and soil crushing in the pre-opened furrow by adopting a field ploughing and managing all-in-one machine to form a planting furrow; and (3) carrying out automatic seed placement, soil covering and film covering planting by adopting a sugarcane planting machine. And (4) fertilizing in a seedling stage and performing physical weeding and micro-hilling. And (5) carrying out fertilization and hilling operation by adopting a field plowing and managing all-in-one machine. (6) chemical weeding and harvesting. (7) leveling the ratoon sugarcane ridges and the sugarcane pockets by adopting a leveling machine, and throwing soil on the ridge surfaces to the two outer sides of the sugarcane pockets; covering the perennial root sugarcane with a film for water retention and heat preservation after leveling; and then managing and harvesting according to the steps (4)-(6), and after each crop of sugarcane is harvested, crushing sugarcane leaves and returning the sugarcane leaves to the field. The application of the method realizes the purposes of carbon sequestration and emission reduction, lodging resistance and sugarcane yield and efficiency increase of soil in the sugarcane field. GUANGXI ZHUANG AUTONOMOUS REGION ACADEMY OF AGRICULTURAL SCIENCES (CN114680010)|GUANGXI ZHUANG AUTONOMOUS REGION ACADEMY OF AGRICULTURAL SCIENCES ([CN]) HUANG JINSHENG|QIN LIPING|ZHOU LIUQIANG|YANG RUIQING|CENG YAN|ZHU XIAOHUI|TAN HONGWEI|HUANG XUEHUA|XIE RULIN|LÜ KUNMING|PENG JIAYU|LI ZHONGNING|LI ZHENGYOU (CN114680010)|HUANG JINSHENG|QIN LIPING|ZHOU LIUQIANG|YANG RUIQING|CENG YAN|ZHU XIAOHUI|TAN HONGWEI|HUANG XUEHUA|XIE RULIN|LÜ KUNMING|PENG JIAYU|LI ZHONGNING|LI ZHENGYOU (CN114680010)|LAI GUANGYE;NANNING LAILAI PATENT AGENCY FIRM|Reg. Nb: 45118 (CN114680010)|The sugar cane high-yield planting method considering both carbon fixation and emission reduction of the soil in the red soil area has the advantages that during the planting process, the local part of the sugar cane land is dug at intervals to reduce the soil disturbance, the disturbance of agricultural implements to the soil is reduced, and the greenhouse gas emission and the oil consumption of the agricultural implements are reduced; the sugarcane seeds are directly attached to the hard ground of the concave groove, and the method of promoting the germination of the sugarcane by using the ground gas is adopted; the soil crushing and throwing combined knife uniformly mixes the straws with soil, so that the problem that the stacking of the straws influences the subsequent farming is reduced, the decomposition of the straws is accelerated, and the organic matter content of the soil is improved; a planting method of deep planting of sugarcane, twice root-tying, high-cultivation lodging resistance, reduction of crater and prevention of rolling of a harvesting machine of a sugarcane pocket; a method for micro-hilling at the sugarcane seedling stage, fixing the growth position of the sugarcane seedlings, increasing the light transmittance and the number of effective stems at the later stage and physically weeding; the perennial root sugarcane is leveled and covered with a film, water retention and heat preservation are realized, the germination of low-position buds is promoted, the emergence rate is improved, and the age limit of the perennial root sugarcane is prolonged.|And the output power of the tractor is unstable, which can cause the quality of stubble leveling of the sugarcane bags to be unstable and reduce the quality of perennial root sugarcane mulching films.|For the lower part is real soil, the upper portion is for throwing the loose soil of going, and the maximum soaks the collection to concave type groove with natural precipitation like this, does benefit to soil and preserves water, and in the operation of ditching, the all-in-one is with fertilizer and the mixing of recess ditch soil, and fertilizer is only limited in recess ditch soil, realizes fertilizer deep fertilization, and recess ditch liquid manure coordinates, improves fertilizer utilization ratio, and sugarcane root system is perpendicular to prick anti lodging for the first time deeply.|In general, the existing agricultural implements of the sugarcane intertillage hiller have poor fusion degree with agriculture, cause grinding, extrusion, pressing and covering to the sugarcane, and are difficult to meet the field operation.| (CN114680010)|1. A high-yield planting method of sugar cane in a red soil area and with consideration of soil carbon sequestration and emission reduction comprises the processes of sugarcane soil preparation, fertilization, seed arrangement, soil covering and film covering, ridging, weeding, harvesting, perennial root sugarcane leveling and film covering, and is characterized in that: the method specifically comprises the following steps:(1) stubble cleaning and pre-ditching: crushing and stubble cleaning are carried out on the residues of the previous crops by adopting a stubble cleaning pre-furrowing machine, and meanwhile, linear pre-furrowing is carried out at a distance of 140cm for positioning the post-process line;(2) local deep scarification and deep ploughing, ditching and base fertilizer application: adopting a tillage and soil preparation pipe all-in-one machine to carry out soil throwing type deep scarification and deep ploughing on broken soil in a ditch which is pre-opened, throwing the broken soil to two sides to form sugarcane planting ditches, wherein the width of each ditch is 70cm, two sides of each sugarcane planting ditch are not ploughed, and meanwhile, applying a special pesticide-fertilizer base fertilizer for sugarcane in the sugarcane planting ditches;(3) seed arrangement, soil covering and film covering: adopting a sugarcane planter to perform automatic seed arrangement, soil covering and film covering planting, arranging two rows of sugarcane seeds in the sugarcane planting ditch, wherein the interval between the two rows of sugarcane seeds is 20 cm;(4) fertilizing in the seedling stage and micro-earthing up by physical weeding: adopting a sugarcane banking machine to apply the seedling fertilizer N120 kg/hm2The method is combined with fertilization, the sugarcane hiller carries out rotary tillage and soil throwing to turn soil on the ridge surface to the ditch to cover 2-5 cm, micro-hilling is carried out, large soil blocks are prevented from extruding seedlings, the growth positions of the sugarcane seedlings can be scattered and positioned, light transmittance and effective stems in the later period are increased, water evaporation can be avoided, secondary root pricking of the sugarcane is promoted, row spacing weeds are rotated off in the rotary tillage hilling process of the sugarcane hiller, and the expenditure of manual weeding and pesticides is reduced;(5) fertilizing in the elongation period and high hilling: fertilizing and ridging operation is carried out by adopting the tillage and field management integrated machine in the step (2); administration ofSugarcane fertilizer, N260 kg/hm2、P2O5 40kg/hm2、K2O 150kg/hm2(ii) a The combined cutter rotating at high speed of the integrated tillage and soil preparation machine crushes soil on the ridge surface originally formed and throws the crushed soil back to the base of the sugarcane plant to obtain high ridging quality with full ridge shape, loose soil and complete and tight weed coverage, and the occurrence of 'fire hills' is reduced; after the hilling loose soil is solidified, the ridge height is 23-26cm, the sugarcane pocket is buried under 20-25 cm of soil, the ridge surface width reaches 60-70 cm, and the ridge bottom width is 108 plus 112cm, so that the lodging resistance of the sugarcane is improved, the crushing damage to the sugarcane pocket during mechanical harvesting is reduced, and the perennial root life is prolonged;(6) chemical weeding and harvesting: after the large hilling, herbicide is sprayed in time for soil sealing, 55 to 70 percent of methyl, ethyl, diuron 2700 and 3600g/hm2Adding water 675L weed stem and leaf directional spray, or using 200g/L glufosinate ammonium 3000-4500 ml/hm2Adding water 675L weed stem leaves, directionally spraying for 1 time, and preventing and treating for 1-2 times according to weed occurrence conditions at later stage; the sugarcane can be harvested in the mature period of the sugarcane process;(7) leveling and covering the perennial root sugarcanes with films: a ridge with the original height of 23-26cm of perennial root sugarcane is cut by a flattening machine with 13-16cm of sugarcane pocket, the ridge surface is smooth and convenient to cover with a film, soil on the ridge surface is thrown to the two outer sides of the sugarcane pocket, and the requirement of subsequent high hilling is met; after the ridge surface is leveled and reduced, the sugarcane is 10-12cm high in ridge, the perennial root sugarcane is covered with a film, water-retaining and heat-preserving, the germination of low-level buds is promoted, the emergence rate is improved, and the perennial root sugarcane age is prolonged; and (5) managing and harvesting according to the processes in the steps (4) to (6), and crushing sugarcane leaves and returning the sugarcane leaves to the field after each batch of sugarcane is harvested.| (CN114680010)|The invention aims to provide a sugar cane high-yield planting method considering both carbon fixation and emission reduction of soil in a red soil area, which is a cultivation mode of 'interval local deep scarification and deep ploughing, uniform mixing of cane leaves and soil, deep planting, micro-cultivation for plant spacing, labor saving, fertilizer application and insect prevention for one time completion by using pesticide and fertilizer, high hilling and perennial root leveling and film covering', reduces the oil consumption of agricultural implement soil preparation and disturbance to soil, reduces organic carbon mineralization of soil, and reduces greenhouse gas emission; the problems that the conventional cultivated land is shallow in cultivation layer, large in intertillage and shallow in earthing up, and sugarcane falls down due to earthing up of a volcanic opening and the like are solved; the phenomenon that the straw piles influence the subsequent farming is reduced; labor cost for applying fertilizer and pesticide is reduced, and utilization rate of the fertilizer is improved; high hilling and perennial root flattening are combined, sugarcane is prevented from lodging, sugarcane bags are prevented from being rolled by a harvesting machine, high-position buds of perennial root sugarcane are prevented from early sprouting, the sugarcane yield is increased, and the perennial root sugarcane age is prolonged; finally achieving the purposes of carbon fixation and emission reduction of the soil of the sugarcane field, lodging resistance, and yield and efficiency increase of the sugarcane. In order to realize the purpose of the invention, the technical scheme is as follows:|The invention relates to the technical field of sugarcane planting, in particular to a high-yield planting method of sugar canes in a red soil area and with the functions of soil carbon sequestration and emission reduction.| (CN114680010)|PERENNIAL ROOT SUGARCANE(100,30)|EMISSION REDUCTION(100,18)|HIGH YIELD(100,18)|SUGAR CANE(100,18)|RED SOIL AREA(100,15)|SOIL CARBON SEQUESTRATION(100,4)|SUGARCANE PLANTING DITCH(73,10)|PERENNIAL ROOT SUGARCANE AGE(57,4)|SUGARCANE POCKET(56,14)|SUGARCANE INTERTILLAGE HILLER(56,1)|ADMINISTRATION OFSUGARCANE FERTILIZER(52,1)|PERENNIAL ROOT SUGARCANE LEVELING(51,2)|SUGARCANE SEEDLING(46,7)|ROTARY TILLAGE SOIL(43,26)|WEEDING EXPENDITURE(41,1)|ROOT SUGARCANE AGE(39,4)|DEEP SCARIFICATION(38,22)|DITCHING PLOW FRAME(38,20)|SUGARCANE HILLER(37,8)|SUGARCANE PLANTER(37,4)|PERENNIAL ROOT FLATTENING(37,1)|PERENNIAL ROOT SUGARCANE QUALITY(37,1)|SUGARCANE POCKET HARVESTING MACHINE(37,1)|ROOT SUGARCANE LEVELING(36,2)|PERENNIAL ROOT LEVELING(36,1)|SUGARCANE(35,68)|SUGARCANE GERMINATION(35,1)|SUGARCANE SEED(34,13)|TRACTOR MIDDLE CANTILEVER(31,15)|SUGARCANE BATCH(31,4)|LEAF SPRAY DIRECTION(31,1)|SUGARCANE LEVELING(31,1)|SOIL EMISSION REDUCTION(30,11)|STUBBLE CLEANING(30,10)|SOIL GUIDING BAFFLE(30,6)|PERENNIAL ROOT SUGARCANE RIDGE(30,5)|HILLING LOOSE SOIL(30,3)|FERTILIZER DEEP FERTILIZATION(30,2)|GROUND(29,126)|PLANTING DEPTH(29,2)|SUGARCANE SOIL(29,2)|FERTILIZER(28,71)|SOIL CRUSHING(28,15)|SUGARCANE DEEP PLANTING(28,3)|FILM COVERING PLANTING(28,2)|INTERVAL LOCAL DEEP SCARIFICATION(28,1)|STRAW STACKING(28,1)|GROUND COVERING(27,11)|LODGING RESISTANCE(27,7)|THROWING LOOSE SOIL(27,2)|SEEDLING FERTILIZER(26,3)|TILLAGE CUTTER(25,6)|DITCHING MARKING PLOW(25,2)|FURROW(25,2)|HARVESTING(25,2)|STRAW PILE(25,1)|SUGARCANE LEAVE(24,6)|FERTILIZER CAROUSEL(24,5)|SUGARCANE LODGING RESISTANCE(24,4)|SUGAR CANE LAND(24,1)|SUGARCANE BAG(24,1)|WEED STEM(24,1)|PLOW ROD(23,18)|DEEP SCARIFICATION PLOW(23,4)|SOIL PLOWING PLATE(23,4)|HILLING REQUIREMENT(23,3)|PERENNIAL ROOT LIFE(23,3)|RECESS DITCH SOIL MIXING(23,2)|AGRICULTURAL IMPLEMENT DISTURBANCE(23,1)|EARLY SPROUTING(23,1)|WEEDING(22,14)|SCRAPING FERTILIZER(22,6)|HM2ADDING(22,2)|RECESS DITCH SOIL(22,2)|AGRICULTURAL IMPLEMENT SOIL(22,1)|INSECT PREVENTION(22,1)|ROTARY TILLAGE(21,18)|ROTARY TILLAGE SHAFT(21,11)|HILLING(21,5)|WEED STEM LEAVE(21,5)|SUGARCANE PLANTING(21,3)|ARC SOIL CRUSHING DISC(21,1)|THROWING COMBINED KNIFE(21,1)|FERTILIZATION(20,13)|STRAW DECOMPOSITION(20,3)|SUBSOILING PLOW MOUNTING SEAT(20,2)|CANE LEAVE(20,1)|CANE LEAVE UNIFORM MIXING(20,1)|STUBBLE QUALITY(20,1)|SOIL THROWING PLATE(19,8)|FARMING(19,3)|SOIL DISTURBANCE(19,2)|ROTARY TILLAGE HILLING(19,1)|PESTICIDE(18,6)|SHAFT SLEEVE(18,4)|PESTICIDE FERTILIZER BASE FERTILIZER(18,3)|SOIL ORGANIC CARBON MINERALIZATION(18,1)|SUGARCANE BASE(18,1)|TILLAGE HILLING(18,1)|MOUNTING ROD(17,21)|TILLAGE(17,18)|CUTTER HANDLE(17,6)|INSTALLING MODE(17,6)|FLATTENING(17,4)|DITCHING PLOW MOUNTING SEAT(17,3)|RIDGING QUALITY(17,3)|FERTILE MOUTHFUL(17,2)|CRATER REDUCTION(17,1)|RIDGE(16,21)|DEEP PLOWING(16,18)|SEEDLING(16,14)|DITCH(16,13)|BROKEN GROUND(16,11)|FILM COVERING(16,11)|CRUSHING(16,8)|HINGE SEAT(16,8)|EMERGENCE RATE(16,4)|FERTILIZER BOARD(16,4)|LOOSE SOIL(16,3)|RECESS DITCH(16,2)|CONCAVE GROOVE HARD GROUND(16,1)|FERTILIZER APPLICATION(16,1)|FERTILIZER PERIPHERY(16,1)|GUIDING FERTILIZER(16,1)|RIDGE BREAKING(15,12)|MICRO HILLING(15,7)|CONICAL HOUSING(15,6)|RACK MIDDLE(15,6)|INTEGRATED TILLAGE(15,5)|BLADE HOLDER(15,3)|FERTILIZER UTILIZATION RATIO(15,2)|CULTIVATION MODE(15,1)|FERTILIZER FILL BOTTOM INTERCOMMUNICATION(15,1)|SCRAPING SOIL(15,1)|AGRICULTURAL IMPLEMENT(14,9)|SUGARCANE YIELD(14,6)|AUTOMATIC SEED ARRANGEMENT(14,4)|MIDDLE CANTILEVER SEAT(14,2)|ROLLING DISC INSTALLATION SEAT(14,2)|SUGARCANE SOIL(14,2)|CULTIVATED LAND(14,1)|CULTIVATION LAYER(14,1)|PLANT SPACE(14,1)|VOLCANIC OPENING(14,1)|STUBBLE(13,15)|SOIL SEALING(13,4)|CRUSHED SOIL BACK(13,3)|FALLING FERTILIZER(13,3)|RIDGE HEIGHT(13,3)|NATURAL PRECIPITATION(13,2)|REAL SOIL(13,2)|CONNECTING FERTILIZER FILL(13,1)|KG HM2THE(13,1)|ORGANIC CARBON MINERALIZATION(13,1)|THREADED SHAFT(12,9)|ARC ROOT CUTTING DISC(12,7)|PRESERVATION(12,4)|CUTTER COMBINATION(12,3)|STIRRING FERTILIZER(12,3)|MOTOR GEARBOX PIVOT(12,2)|MANAGEMENT INTEGRATED MACHINE(12,1)|HYDRAULIC OIL CYLINDER(11,10)|SQUARE SHAFT(11,8)|CARBON FIXATION(11,5)|CONCAVE GROOVE(11,4)|CUTTER HOLDER(11,3)|SUGARCANE FIELD SOIL(11,3)|FERTILIZER BOX FRAME(11,2)|FERTILIZER BUCKET BOTTOM(11,2)|INTERTILLAGE(11,2)|LIQUID MANURE COORDINATE(11,2)|MAXIMUM SOAK(11,2)|TURNTABLE III(11,1)|UNIFORM MIXING(11,1)|GEAR TRANSMISSION BOX(10,14)|PLANTING(10,11)|RIDGE SURFACE(10,10)|BASE FERTILIZER(10,9)|ARC CIRCULAR BLADE(10,5)|ELONGATION PERIOD(10,4)|FERTILIZER CIRCULAR ROTATING DISC(10,4)|LATE PERIOD(10,4)|MATURITY PERIOD(10,4)|GLUFOSINATE AMMONIUM(10,3)|OCCURRENCE CONDITION(10,3)|ROLLING DISC MOUNTING SEAT(10,3)|AGRICULTURE(10,2)|CULTIVATION(10,2)|CUTTING RIDGE(10,2)|LEVELING(10,2)|STRAW(10,2)|EXTRUSION(10,1)|GRINDING(10,1)|PRE OPENED DITCH(10,1)|SHALLOW(10,1)|SOIL GAS(10,1)|COVERING COMBINED MACHINE(9,5)|HERBICIDE(9,5)|STEM(9,4)|AGRICULTURAL IMPLEMENT OIL CONSUMPTION(9,3)|DIURON(9,3)|SEED ARRANGEMENT(9,3)|STIRRING BLADE(9,3)|HARD SOIL(9,2)|PRESERVE WATER(9,2)|SOIL CUTTING OPENING(9,2)|SUGARCANE INSECTICIDE FERTILIZER(9,2)|SUGARCANE PESTICIDE FERTILIZER(9,2)|AGE(9,1)|ROOT CUTTING ROTATING SHAFT(8,14)|INSTALLATION ROTATING SHAFT(8,10)|TRACTOR SIDE CANTILEVER(8,10)|ROTATING SHAFT SEAT(8,7)|OIL CONSUMPTION(8,5)|RIDGING OPERATION(8,5)|DITCHING FARMING RESISTANCE(8,4)|SUGARCANE SPROUT(8,4)|COVERAGE(8,3)|DEEP LOOSENING PLOW(8,3)|GREENHOUSE GAS EMISSION(8,3)|LODGING(8,3)|SPRAYING(8,3)|SUGARCANE(8,3)|SUGARCANE PROCESS MATURE PERIOD(8,3)|CYLINDER SEAT(8,2)|SOIL CARBON SEQUESTRATION FUNCTION(8,2)|FUSION DEGREE(8,1)|PLANTING(8,1)|SHORT TOOTH(7,9)|FERTILIZER CIRCULAR TURNTABLE(7,4)|LARGE HILLING(7,4)|LIGHT TRANSMITTANCE(7,4)|SCRIBING PLOW(7,4)|WEED(7,4)|FERTILE CAROUSEL(7,3)|FIRE(7,3)|FULL RIDGE SHAPE(7,3)|GEARBOX ROTATING SHAFT(7,3)|MECHANICAL HARVESTING(7,3)|PERENNIAL SUGARCANE ROOT CUTTING(7,3)|PLANTED SUGARCANE(7,3)|RIDGE BOTTOM WIDTH(7,3)|STRETCHING MODE(7,3)|SPLASHING(7,2)|SUGARCANE NUTRIENT REQUIREMENT(7,2)|FLAT ARRANGING MACHINE(7,1)|PERENNIAL SUGARCANE MULCHING(7,1)|TILLAGE SOIL THROWING CUTTER(7,1)|GROUND BREAKING(6,7)|K2O(6,5)|LOCKING NUT(6,5)|P2O(6,5)|SOIL LOOSENING(6,5)|SUGARCANE FIELD(6,5)|COUPLER(6,4)|SUGARCANE POCKET OUTER SIDE(6,4)|ARC ROTARY TILLAGE BLADE(6,3)|LUG RING(6,3)|ROD SEAT INSTALLATION PLATE(6,3)|STUBBLE BROKEN STRAW(6,2)|LEVELING PERENNIAL SUGARCANE(6,1)|RATOON SUGARCANE RIDGE(6,1)|RATOON SUGARCANE RIDGING HEIGHT(6,1)|SUGARCANE FARMER INCOME(6,1)|TRACTOR OUTPUT POWER(6,1)|WUMING ALTAR TOWN(6,1)|POWER INPUT SHAFT(5,15)|LOCKING PLATE(5,11)|ANGLE ADJUSTING ROD(5,7)|FERTILIZER OUTER WALL(5,7)|KG HM(5,7)|POWER SHAFT(5,7)|MOUNTING LONG HOLE(5,4)|ORGANIC MATTER CONTENT(5,4)|WATER RETENTION(5,4)|EARTH SCRAPER(5,3)|KNIFE HOLDER(5,3)|FERTILIZER FERMENTATION(5,2)|LIFTING(5,2)|MACHINE ADVANCING DIRECTION(5,2)|PESTICIDE EXPENDITURE(5,2)|PLANTING SUGARCANE(5,2)|ROOT BURNING PHENOMENA(5,2)|SUGARCANE BUD(5,2)|SUGARCANE ROOT SYSTEM(5,2)|WHEREABOUTS FERTILIZER CONNECTION(5,2)|ARC HACK DISH(5,1)|DEEP DITCHING DRAGGING(5,1)|DEEP DITCHING PLANTING(5,1)|DEEP PLOWING SUBSOILING HACK(5,1)|FERTILIZER BOX OUTER WALL(5,1)|HIGH CULTIVATION LODGING RESISTANCE(5,1)|LAND CIRCULATION POPULARIZATION(5,1)|PERENNIAL SUGARCANE GROWTH(5,1)|PLANTED PERENNIAL ROOT(5,1)|ROTARY TILLAGE DEEP SCARIFICATION(5,1)|SUGARCANE LEAF NUTRIENT(5,1)|SUGARCANE PLANTING MANAGEMENT(5,1)|SUGARCANE RIDGE ROOT(5,1)|SUGARCANE SEEDLING GROWTH(5,1)|DRIVING SHAFT(4,12)|FILM FRAME(4,10)|LONG TOOTH(4,9)|MULCHING FILM SIDE(4,9)|CONNECTING ROD SHAFT(4,6)|ADJUSTING THREAD CONNECTING ROD(4,5)|FILM SHAFT(4,5)|SUGARCANE RIDGE SIDE(4,5)|GEARBOX III(4,4)|INSTALLATION POLE(4,4)|KNIFE SEAT(4,4)|ARC SHAPED SOIL(4,3)|DEEP TILLAGE(4,3)|FERTILIZER ROTATING DISC(4,3)|FIXED MOUNTING HOLE(4,3)|LOW LEVEL BUD GERMINATION(4,3)|RIDGE WIDTH SURFACE(4,3)|SPRAYING DIRECTION(4,3)|SUGAR CANE HIGH YIELD(4,3)|THREADED CONNECTION(4,3)|MUD(4,2)|PLUS ROTARY TILLAGE(4,2)|SOIL THROWING KNIFE(4,2)|SUGARCANE HILLER HILLING(4,2)|ARC ROTARY TILLAGE KNIFE(4,1)|CRUSHED SUGARCANE LEAVE(4,1)|DEEP DITCH PLANTING(4,1)|DITCHING PLANTING ROW SPACING(4,1)|FARMER CULTIVATION(4,1)|FERTILE CIRCLE CAROUSEL III(4,1)|FERTILIZER BOX FERTILIZER OUTLET(4,1)|FIELD CULTIVATION(4,1)|HILLING SUGARCANE(4,1)|INTERTILLAGE RIDGING MACHINE(4,1)|INTERTILLAGE WEEDING(4,1)|LARGE SOIL BLOCK(4,1)|LOW POSITION BUD GERMINATION(4,1)|METOLACHLOR DIURON(4,1)|NON SOIL CUTTING(4,1)|PERENNIAL ROOT AGE(4,1)|PLOW SHOVEL(4,1)|RATOON SUGARCANE ROOT CUTTING(4,1)|REALIZING SUBSOILING(4,1)|ROOT SUGARCANE PLOT(4,1)|SCARIFICATION PLOW INSTALLATION MODE(4,1)|SCARIFICATION PLOW MATCHING MODE(4,1)|SCARIFICATION PLOW MOUNTING SEAT(4,1)|STUBBLE CUTTING SOIL(4,1)|SUGARCANE DITCH(4,1)|SUGARCANE MECHANIZED PRODUCTION(4,1)|THROWING SOILCAN(4,1)|TIME COMPLETION(4,1)|POWER OUTPUT SHAFT(3,12)|SUPPORT FRAME(3,10)|MACHINE COMBINATION(3,9)|LABOR COST(3,8)|FIELD MANAGEMENT(3,6)|RACK III(3,5)|PLANTER(3,4)|SUGARCANE SEED TWO ROW(3,4)|FILM PRESSING WHEEL(3,3)|OBTUSE ANGLE(3,3)|SOIL DEPTH(3,3)|SQUARE AXLE(3,3)|TRACTION RESISTANCE(3,3)|UTILIZATION RATE(3,3)|WHEEL CARRIER(3,3)|CANTILEVER SIDE SEAT(3,2)|DEEP PLANTING(3,2)|ECOLOGICAL BENEFIT(3,2)|EMPTY SOIL(3,2)|EXTRA IRRIGATION(3,2)|MOISTURE EVAPORATION(3,2)|ROOT CUTTING MOUNTING ANGLE(3,2)|ROTATING DIRECTION(3,2)|SEED BURNING(3,2)|WALKING ROUTE(3,2)|WELDED FASTENING(3,2)|ADOPTED PLOWING MODE(3,1)|ADOPTED TILLAGE(3,1)|DEEP GROOVE PLANTING(3,1)|DOMESTIC SUGARCANE SUPPLY(3,1)|EARLY GERMINATION(3,1)|ENCRYPTED SAMPLING(3,1)|FARMER HABIT(3,1)|FERTILE FILL BOTTOM INTERCOMMUNICATION(3,1)|FERTILIZER BOTTOM INTERCOMMUNICATION(3,1)|FERTILIZER DISCHARGING ROTARY DISC(3,1)|GROUND LEVELING(3,1)|HACK REGULATION(3,1)|HM2THE NET INCOME(3,1)|MECHANIZATION PRODUCTION IDEA(3,1)|NATIVE ROLLING DISC(3,1)|NONSOIL CUTTING(3,1)|PERENNIAL ROOT CROP(3,1)|PESTICIDE MECHANICAL TILLAGE(3,1)|PLOW HEIGHT ADJUSTMENT(3,1)|PLOW ROD SEAT(3,1)|RIDGE BREAKING RIDGING(3,1)|SCARIFICATION DEPTH(3,1)|SOIL CRUSHING CAPABILITY(3,1)|SOIL CUT MOUTHFUL(3,1)|SOIL GUIDE BAFFLE(3,1)|SOIL ROLLING DISC(3,1)|SOIL SPLASH(3,1)|STRAW STALK ROTARY CULTIVATOR(3,1)|STUMPING CUTTER(3,1)|SUGARCANE ABSORPTION(3,1)|SUGARCANE CULTIVATION TECHNICAL MODE(3,1)|SUGARCANE ELONGATION PERIOD(3,1)|SUGARCANE MARKET PRICE(3,1)|SUGARCANE PLANTING LABOR COST(3,1)|SUGARCANE PLANTING MODE(3,1)|SUGARCANE PRODUCTION MANAGEMENT(3,1)|SUGARCANE SPLIT(3,1)|SUGARCANEAND MATURE PERIOD(3,1)|TOC INSTRUMENT(3,1)|TRACTOR PLANTING(3,1)|TURNOVER SOIL(3,1)|UPPER STUBBLE SUGARCANE RIDGE(3,1)|UPPER STUBBLE SUGARCANE RIDGING(3,1)|WEED STEM LEAF(3,1)|WILLOW CITY DOUBLE ROW(3,1)|YEARS2THE AMPLIFICATION(3,1)|RACK FRONT END(2,13)|RACK REAR END(2,8)|TENSION SPRING(2,5)|SUPPORTING FRAME(2,3)|ARC SOIL(2,2)|DEGRADABLE FILM(2,2)|FERTILIZER ACTION(2,2)|FILM TENSION(2,2)|GROUND COVER(2,2)|INSTALLATION ROD(2,2)|KNIFE HANDLE(2,2)|LAND HALF(2,2)|SOIL BREAKING FARMING AREA(2,2)|SUGARCANE SEEDLING GROWING POSITION(2,2)|SUGARCANE SURVIVAL RATE(2,2)|BREAKING RIDGE(2,1)|CHEMICAL FERTILIZER TILLAGE(2,1)|CIRCULATING DRY LAND(2,1)|DIG SOIL(2,1)|ECONOMIC BENEFIT(2,1)|FERTILIZER BOX III(2,1)|FERTILIZER FRAME(2,1)|FERTILIZER GUIDE PIPE(2,1)|FERTILIZER INJECTION(2,1)|FERTILIZER SCRAPING PLATE FRAME(2,1)|HACK BACK SOIL REGULATION(2,1)|HILLING DEPTH(2,1)|HINGED SEAT(2,1)|HYDRAULIC CYLINDER JAR SEAT(2,1)|MACHINE TILLAGE(2,1)|MECHANIZATION PLANTING DIRECTION(2,1)|MOUNTING ROD TAIL END(2,1)|OUTPUT POWER(2,1)|PLACING MULCHING FILM(2,1)|POTASSIUM DICHROMATE OXIDATION CAPACITY(2,1)|REALIZING DIFFICULT WINDING(2,1)|ROTARY TILLAGE WORKING RESISTANCE(2,1)|SEAMLESS BUTT JOINT(2,1)|SIMULTANEOUSLY COLLECTING SOIL(2,1)|SOLID HERB GROWING(2,1)|STEM INJURY(2,1)|STUBBLE CLEANING ROTARY BLADE(2,1)|STUMPING MACHINE(2,1)|SUGARCANE HEAD(2,1)|SUGARCANE ROW(2,1)|SUGARCANE YIELD ANALYSIS(2,1)|THROW SOIL(2,1)|TILLAGE INTEGRATED MACHINE(2,1)|TOGGLE BLADE(2,1)| (CN114680010)|1. A high-yield planting method of sugar cane in a red soil area and with consideration of soil carbon sequestration and emission reduction comprises the processes of sugarcane soil preparation, fertilization, seed arrangement, soil covering and film covering, ridging, weeding, harvesting, perennial root sugarcane leveling and film covering, and is characterized in that: the method specifically comprises the following steps:|(1) stubble cleaning and pre-ditching: crushing and stubble cleaning are carried out on the residues of the previous crops by adopting a stubble cleaning pre-furrowing machine, and meanwhile, linear pre-furrowing is carried out at a distance of 140cm for positioning the post-process line;|(2) local deep scarification and deep ploughing, ditching and base fertilizer application: adopting a tillage and soil preparation pipe all-in-one machine to carry out soil throwing type deep scarification and deep ploughing on broken soil in a ditch which is pre-opened, throwing the broken soil to two sides to form sugarcane planting ditches, wherein the width of each ditch is 70cm, two sides of each sugarcane planting ditch are not ploughed, and meanwhile, applying a special pesticide-fertilizer base fertilizer for sugarcane in the sugarcane planting ditches;|(3) seed arrangement, soil covering and film covering: adopting a sugarcane planter to perform automatic seed arrangement, soil covering and film covering planting, arranging two rows of sugarcane seeds in the sugarcane planting ditch, wherein the interval between the two rows of sugarcane seeds is 20 cm;|(4) fertilizing in the seedling stage and micro-earthing up by physical weeding: adopting a sugarcane banking machine to apply the seedling fertilizer N120 kg/hm2The method is combined with fertilization, the sugarcane hiller carries out rotary tillage and soil throwing to turn soil on the ridge surface to the ditch to cover 2-5 cm, micro-hilling is carried out, large soil blocks are prevented from extruding seedlings, the growth positions of the sugarcane seedlings can be scattered and positioned, light transmittance and effective stems in the later period are increased, water evaporation can be avoided, secondary root pricking of the sugarcane is promoted, row spacing weeds are rotated off in the rotary tillage hilling process of the sugarcane hiller, and the expenditure of manual weeding and pesticides is reduced;|(5) fertilizing in the elongation period and high hilling: fertilizing and ridging operation is carried out by adopting the tillage and field management integrated machine in the step (2); administration ofSugarcane fertilizer, N260 kg/hm2、P2O5 40kg/hm2、K2O 150kg/hm2(ii) a The combined cutter rotating at high speed of the integrated tillage and soil preparation machine crushes soil on the ridge surface originally formed and throws the crushed soil back to the base of the sugarcane plant to obtain high ridging quality with full ridge shape, loose soil and complete and tight weed coverage, and the occurrence of 'fire hills' is reduced; after the hilling loose soil is solidified, the ridge height is 23-26cm, the sugarcane pocket is buried under 20-25 cm of soil, the ridge surface width reaches 60-70 cm, and the ridge bottom width is 108 plus 112cm, so that the lodging resistance of the sugarcane is improved, the crushing damage to the sugarcane pocket during mechanical harvesting is reduced, and the perennial root life is prolonged;|(6) chemical weeding and harvesting: after the large hilling, herbicide is sprayed in time for soil sealing, 55 to 70 percent of methyl, ethyl, diuron 2700 and 3600g/hm2Adding water 675L weed stem and leaf directional spray, or using 200g/L glufosinate ammonium 3000-4500 ml/hm2Adding water 675L weed stem leaves, directionally spraying for 1 time, and preventing and treating for 1-2 times according to weed occurrence conditions at later stage; the sugarcane can be harvested in the mature period of the sugarcane process;|(7) leveling and covering the perennial root sugarcanes with films: a ridge with the original height of 23-26cm of perennial root sugarcane is cut by a flattening machine with 13-16cm of sugarcane pocket, the ridge surface is smooth and convenient to cover with a film, soil on the ridge surface is thrown to the two outer sides of the sugarcane pocket, and the requirement of subsequent high hilling is met; after the ridge surface is leveled and reduced, the sugarcane is 10-12cm high in ridge, the perennial root sugarcane is covered with a film, water-retaining and heat-preserving, the germination of low-level buds is promoted, the emergence rate is improved, and the perennial root sugarcane age is prolonged; and (5) managing and harvesting according to the processes in the steps (4) to (6), and crushing sugarcane leaves and returning the sugarcane leaves to the field after each batch of sugarcane is harvested.|2. The high-yield planting method of sugar cane in the red soil area with carbon sequestration and emission reduction of soil as claimed in claim 1, which is characterized in that: the field cultivation and management integrated machine comprises a rack (1) and a gear box (11), wherein the gear box (11) is installed above the middle of the rack (1), power output shafts (25) are installed on the left side and the right side of the gear box (11) respectively, and a power input main shaft (12) capable of being connected with a power shaft of a tractor is installed at the front end of the gear box (11); a side cantilever seat (15) used for being connected with a side cantilever of a tractor in an installing mode is arranged at the front end of the rack (1), and a middle cantilever seat (9) used for being connected with a middle cantilever of the tractor in an installing mode is arranged above the front end of the rack (1) through a support (10); two sides of the lower part of the front end of the rack (1) are respectively provided with a subsoiling plough (17) through a subsoiling plough mounting seat (16), a gear transmission case (14) is fixed on the rack (1) right behind each subsoiling plough (17), the upper end of the gear transmission case (14) is provided with a power input shaft (13), and the power input shaft (13) is connected with a power output shaft (25) through a coupling (26); two sides of the lower end of the gear transmission box (14) are respectively provided with a driving shaft (20) with the rotating direction opposite to the advancing direction of the all-in-one machine, and a plurality of rotary tillage soil throwing knives (18) are arranged on the driving shaft (20) through a knife holder (19); a baffle (22) is installed at the lower part of the rack (1) above the rotary tillage soil throwing knife (18), one side of the baffle (22) far away from the gear transmission case (14) is hinged with a soil guiding baffle (21) through a hinge (23), the soil guiding baffle (21) is also connected with the rack (1) through an angle adjusting rod (24), and the angle adjusting rod (24) can adjust the opening angle of the soil guiding baffle (21); the frame (1) is provided with a fertilizing device which can automatically guide fertilizer to the rear side of the gear transmission case (14).|3. The high-yield planting method of sugar cane in the red soil area with carbon sequestration and emission reduction of soil as claimed in claim 2, characterized in that: three groups of rotary tillage soil throwing blades (18) are uniformly arranged on the driving shaft (20) through a blade holder (19), each group of rotary tillage soil throwing blades (18) consists of three rotary tillage soil throwing blades (18), and the three rotary tillage soil throwing blades (18) are uniformly arranged on the blade holder (19); the rotary tillage soil throwing cutter (18) comprises an L-shaped arc-shaped rotary tillage cutter (27) and a soil throwing plate (28), a cutter handle (29) is arranged at the straight end of the L-shaped arc-shaped rotary tillage cutter (27), a mounting hole (30) for connecting and fixing the cutter handle (29) with the cutter holder (19) is formed in the cutter handle (29), and the soil throwing plate (28) is fixed on the arc surface of the non-soil cutting side of the arc-shaped end of the L-shaped arc-shaped rotary tillage cutter (27); the soil throwing plate (28) and the knife face of the L-shaped arc rotary blade (27) are arranged in an obtuse angle.|4. The high-yield planting method for the sugar cane in the red soil area with carbon sequestration and emission reduction of the soil as claimed in claim 2, characterized in that: the deep scarification plough (17) comprises a plough rod (34), a long tooth (36) extending forwards is fixed on the front side of the bottom end of the plough rod (34), soil ploughing plates (32) inclining downwards from back to front are respectively arranged on the left side and the right side of the bottom end of the plough rod (34), and a short tooth (31) extending forwards is fixed on the side, far away from the plough rod (34), of the front end of each soil ploughing plate (32); the left side and the right side of a plow rod (34) above the soil plowing plate (32) are respectively provided with a side plate (33) which is opened backwards; the upper end of the plow lever (34) is provided with a fixed mounting hole (35) which is used for connecting and fixing the deep scarification plow mounting seat (16); fertilizing device include fertilizer box (8), install in frame (1) fertilizer box (8) through fertilizer box frame (2), install a motor gear box (5) on frame (1) of fertilizer box (8) lower part respectively, all be fixed with one in the pivot of motor gear box (5) and cover fertilizer box (8) and go out lower fertilizer carousel (7) of fertile mouthful, the outer wall of fertilizer box (8) is provided with one and has and is used for scraping the fertilizer in fertilizer carousel (7) down and scrape fertilizer board (6), scrape and install on frame (1) of fertilizer board (6) below and be used for connecing lower fertilizer fill (4) of whereabouts fertile, the bottom intercommunication of lower fertilizer fill (4) has conduit (3), conduit (3) extend the rear side of gear drive case (14).|5. The high-yield planting method of sugar cane in the red soil area with carbon sequestration and emission reduction of soil as claimed in claim 1, which is characterized in that: the stubble-cleaning pre-furrowing machine is driven by a tractor in a traction way and is characterized in that: the front end of the rack I (42) is provided with a side cantilever seat I (46) which is used for being connected with a side cantilever of a tractor in an installing way, and a middle cantilever seat I (50) which is used for being connected with a middle cantilever of the tractor in an installing way is arranged above the front end of the rack I (42) through a support I (51); two sides of the front end of the frame I (42) are respectively provided with a front scarification plough (54) through a scarification plough mounting seat (55), and the rear end frame I (42) at the left side and the right side of each front scarification plough (54) is respectively provided with a rear scarification plough (52) through the scarification plough mounting seat (55); the rear end of the rack I (42) is provided with a ditching plow frame (57), the ditching and marking plow (53) is arranged on the ditching plow frame (57) behind each front scarification plow (54) through a ditching plow mounting seat (56), the gear box I (48) is arranged above the middle of the rack I (42), the left side and the right side of the gear box I (48) are respectively provided with a power output shaft I (47), and the front end of the gear box I (48) is provided with a power input main shaft I (49) which can be connected with a power shaft of a tractor; the left side and the right side of the rack I (42) are symmetrically and fixedly provided with a gear transmission box I (38), the upper end of the gear transmission box I (38) is provided with a power input shaft I (44), and the power input shaft I (44) is connected with a power output shaft I (47) through a coupler I (45); a rotary tillage shaft (40) is arranged between the lower ends of the two gear transmission boxes I (38) through a bearing with a base (39), the rotary tillage shaft (40) is connected with a gear in the gear transmission box I (38), and stubble cleaning rotary blades (41) are arranged on the rotary tillage shaft (40).|6. The high-yield planting method of sugar cane in the red soil area with carbon sequestration and emission reduction of soil as claimed in claim 5, characterized in that: the front end of the gear transmission box I (38) is provided with a soil breaking plough (37); a baffle I (43) for preventing mud from splashing is arranged on the rack I (42); the ditching plow frame (57) is hinged at the rear end of the machine frame I (42), the ditching plow frame (57) is further hinged with the machine frame I (42) or the gear box I (48) through a hydraulic oil cylinder (58), a cylinder seat of the hydraulic oil cylinder (58) is hinged with the machine frame I (42) or the gear box I (48), a piston rod of the hydraulic oil cylinder (58) is hinged with the ditching plow frame (57), the ditching plow frame (57) is controlled to turn through the hydraulic oil cylinder (58), and lifting and lowering of the ditching marking plow (53) are controlled.|7. The high-yield planting method of sugar cane in the red soil area with carbon sequestration and emission reduction of soil as claimed in claim 1, which is characterized in that: the perennial root sugarcane is subjected to film covering, water retention and heat preservation, and a perennial root sugarcane root cutting, ridge breaking, fertilizing and film covering combined machine is adopted, the perennial root sugarcane root cutting, ridge breaking, fertilizing and film covering combined machine comprises a rack III (89), a side cantilever seat III (88) used for being connected with a side cantilever of a tractor in an installing mode is arranged at the front end of the rack III (89), and a middle cantilever seat III (93) used for being connected with a middle cantilever of the tractor in an installing mode is arranged above the front end of the rack III (89); a fertilizer box III (95) is arranged on the rack III (89) through a fertilizer box rack III (94), a gear box III (92) driven by a hydraulic motor III (91) is arranged on the rack III (89) at the lower part of the fertilizer box III (95), and a lower fertilizer circular rotating disc III (97) covering a fertilizer outlet at the bottom of the fertilizer box III (95) is fixed on a rotating shaft of the gear box III (92); two sides of the outer wall of the fertilizer box III (95) are respectively provided with a fertilizer scraping plate III (96) for scraping the fertilizer in the lower fertilizer circle turntable III (97), two sides of the outer wall of the fertilizer box III (95) are respectively provided with a lower fertilizer bucket III (98) for receiving the falling fertilizer, and the bottom of the lower fertilizer bucket III (98) is communicated with a fertilizer guide pipe III (110); two sides of the front end of the rack III (89) are respectively provided with a root cutting and soil breaking rolling disc (87) for cutting ridges and roots on two sides of a sugarcane ridge through rolling disc mounting seats (90), and the fertilizer guide pipe III (110) extends to the rear outer side of the root cutting and soil breaking rolling disc (87); a film frame (109) is installed at the lower part of the rear end of the frame III (89), a film shaft (108) for placing mulching films is installed on the film frame (109), and film pressing wheels (106) for rolling the two sides of the mulching films are installed on the rear side of the film frame (109) through a wheel carrier (107); two sides of the rear end of the rack III (89) are respectively provided with a hinge seat (99), the two hinge seats (99) are respectively hinged with a mounting rod (103) extending backwards, the bottom end of the mounting rod (103) is connected with a tension spring (100) connected with the bottom of the hinge seat (99), and the lower part of the rear end of the mounting rod (103) is provided with a soil crushing and soil returning rolling disc (105) for scraping soil on two sides of a mulching film; the middle part of the rear end of the rack III (89) is connected with a support frame (102) extending backwards, and two sides of the support frame (102) are respectively connected with mounting rods (103) at two sides through a threaded adjusting connecting rod (101) for limiting.|8. The high-yield planting method of sugar cane in the red soil area with carbon sequestration and emission reduction of soil as claimed in claim 7, characterized in that: the soil crushing and soil returning rolling disc (105) comprises a rotating shaft seat (120) and an installation rotating shaft (125), the installation rotating shaft (125) is installed in the rotating shaft seat (120) through a bearing, an arc-shaped soil returning disc (124) is installed on the installation rotating shaft (125) in a stretching mode, the top end of the rotating shaft seat (120) is fixedly connected with a connecting shaft (121), a square shaft body (122) and a threaded shaft body (123) are arranged at the top end of the connecting shaft (121), and the threaded shaft body (123) is located at the top of the square shaft body (122); the connecting shaft (121) is connected with the mounting rod (103) through a shaft sleeve, the shaft sleeve is vertically welded and fixed at the tail end of the mounting rod (103), a connecting lug is arranged at the upper end of the shaft sleeve, a long hole or a plurality of connecting holes are formed in the connecting lug, a locking plate (104) is arranged on a square shaft body (122) after the connecting shaft (121) penetrates through the shaft sleeve, and a locking nut is arranged on a threaded shaft body (123); the root cutting and soil breaking rolling disc (87) comprises a root cutting rotating shaft (113) and a rod seat (115), the root cutting rotating shaft (113) is installed in the rod seat (115) through a root cutting rotating shaft bearing (114), an arc root cutting disc (118) is installed at the extending end of the root cutting rotating shaft (113), a rod seat installation plate (116) which is used for being connected with the rolling disc installation seat (90) through bolts is arranged at the top end of the arc root cutting disc (118) through a connecting rod shaft, and the rod seat installation plate (116) is located at the top of the connecting rod shaft; the rod seat mounting plate (116) is provided with a mounting long hole (117), the mounting long hole (117) is arranged to facilitate adjustment of the mounting position of the rolling disc mounting seat (90), and the mounting angle of the root cutting and soil breaking rolling disc (87) is realized; a plurality of soil cutting openings (119) are uniformly distributed on the edge of the arc soil crushing disc (23); the thread adjusting connecting rod (101) comprises a connecting screw I (126), a screw connecting seat (127) and a connecting screw II (129), the screw connecting seat (127) is a hollow long connecting seat, the connecting screw I (126) and the connecting screw II (129) are respectively in threaded connection with two ends of the screw connecting seat (127), the connecting screw I (126) is hinged to the mounting rod (103) through a connecting lug ring, the connecting screw II (129) is hinged to the supporting frame (102) through the connecting lug ring, and a locking nut (128) used for locking the connecting screw II (129) and the screw connecting seat (127) is mounted on the connecting screw II (129); the middle part of the lower fertilizer round turntable III (97) is provided with a vertical conical housing (111) for preventing fertilizer from being accumulated in the middle part of the lower fertilizer round turntable III (97), and the conical housing (111) is arranged for guiding the fertilizer falling from the inside of the fertilizer box III (95) to the periphery of the lower fertilizer round turntable III (97); the conical housing (111) is provided with a stirring blade (112) for stirring fertilizer. (CN114680010)|TECHNICAL FIELD|[0001] The invention relates to the technical field of sugarcane planting, in particular to a high-yield planting method of sugar canes in a red soil area and with the functions of soil carbon sequestration and emission reduction.|BACKGROUND ART|[0002] Sugarcane, (academic name:Saccharumofficinarum) Saccharum officinarum, a large and solid herb growing for many years. The root is strong and developed. The height of the stalk is 3-6 m. The sugarcane is suitable for being planted in places with fertile soil, sufficient sunlight and large temperature difference in winter and summer. The sugarcane isThe most important sugar crops in China occupy a very important position in tropical regions. Sugarcane is perennial root crop, and can be harvested for 3-7 years after being managed in place and newly planted once. Newly planted sugarcane needs to be cultivated, sowed, intertillage weeding, fertilizing and hilling, harvested and other production links in sugarcane production, and perennial root sugarcane also needs to be cultivated, ploughed, weeding, fertilizing, hilling, harvested and other production links.|[0003] The traditional sugarcane planting mode is a man-and-animal-powered working mode, is low in efficiency and high in labor intensity, and has a great limiting effect on scale management of sugarcane production in China. With the increasing of labor cost in rural areas and the popularization of land circulation and mechanization, sugarcane planting develops towards the direction of mechanization planting, and people put forward a production idea of mechanization in the whole process of sugarcane production in recent years. However, due to factors such as drought in climate, degradation of variety, chemical fertilizer abuse, small scale and the like, especially mismatch between agricultural machinery and agricultural implements, mismatch between agricultural implements and agricultural implements, and mismatch between agricultural implements and agriculture, effective, ideal and seamless butt joint of whole-process mechanized operations of sugarcane planting production still cannot be realized, so that the labor cost of sugarcane planting rises dramatically, the income of sugarcane farmers is reduced sharply, the sugarcane planting area is reduced, the yield is reduced, and the supply of domestic sugarcane is seriously influenced.|[0004] Actual planting research finds that the current mechanical sugarcane planting management mode mainly has the following defects.|[0005] 1. In the traditional mechanized planting management process of the sugarcane, a large-scale tractor with high horsepower and high strength is mainly used for deep ploughing, rotary tillage, deep scarification and rotary tillage in the machine tillage and soil preparation process, and the defects that after the rotary tillage operation, the scarification depth is more than 25cm, the tillage layer is shallow, the sugarcane is shallow in root, the continuous utilization capability of water and fertilizer is poor, the sugarcane is easy to fall down, and the yield is low are caused. Although the ridge smashing machine is adopted for ridge smashing deep ploughing, the ploughing depth can reach 30-40 cm, the ridge smashing ploughing and deep ploughing plus rotary tillage, deep scarification plus rotary tillage are the same and need a tractor with larger horsepower to operate, the oil consumption is large, the energy saving and emission reduction are not facilitated, and the adopted ploughing mode is that the whole field soil is turned over generally, the soil disturbance is increased, so that the closed accumulation organic carbon protected by aggregates is rapidly utilized by microorganisms after being exposed, the organic carbon is mineralized, and the organic carbon is discharged and discarded in the form of carbon dioxide.|[0006] 2. In the aspect of mixing the sugarcane leaves and the soil, the deep ploughing operation can bury the sugarcane leaves into the subsoil, but the sugarcane leaves are decomposed in the subsoil layer, the nutrients of the sugarcane leaves are not easy to be absorbed and utilized by the sugarcane in the current year, and the deep ploughing operation mainly aims at the operation of directly ploughing and re-planting the sugarcane after crushing, but is not suitable for continuously lodging the root sugarcane plots. Because of the large amount of sugarcane leaves in the field, the rotary cultivator and the ridge smashing machine can not disperse the sugarcane leaves, so that the sugarcane leaves are piled up, soil is possibly lifted, the moisture in the soil is evaporated more quickly, the absorption of the sugarcane to moisture and nutrients is not facilitated, and the growth of sugarcane seedlings is influenced.|[0007] 3. The ridge-breaking ridging amount of the small ridging or perennial root sugarcane is large, soil extrudes the sugarcane to different degrees, tillering and stem forming rate of the sugarcane are influenced, and the group structure of the sugarcane is unreasonable; and the soil is sealed by adopting a herbicide after hilling, so that the labor and pesticide costs are increased.|[0008] 4. The intertillage large ridging mainly adopts a plough shovel type, spiral type or disc type intertillage ridging machine to carry out ditching ridging. The plow-shovel type banking machine has poor soil crushing capability; the spiral mechanical ridge shape has poor adaptability and large energy consumption, the soil throwing flow direction is not easy to control, the soil splashes at a high speed, and the injury of stems and leaves of crops and the personal safety are easy to cause; the disc type hiller is used for hilling sugarcane fields with hard soil, and the hilling depth and effect of the disc type hiller are inferior to those of a spiral type hiller. In general, the existing agricultural implements of the sugarcane intertillage hiller have poor fusion degree with agriculture, cause grinding, extrusion, pressing and covering to the sugarcane, and are difficult to meet the field operation.|[0009] 5. The perennial root sugarcane stumping mainly utilizes a stumping cutter head of a stumping machine to stump, and only can cut the sugarcane heads on the ground due to the horizontal rotation of the cutter head, so that the early germination of high-position buds is easily induced, the sugarcane seedlings are slender, and the germination of the low-position buds of the base parts is inhibited. And the output power of the tractor is unstable, which can cause the quality of stubble leveling of the sugarcane bags to be unstable and reduce the quality of perennial root sugarcane mulching films.|[0010] In order to better realize the mechanized production of the sugarcane, the high-yield sugarcane planting technology integrating the fine variety and fine method technical mode is designed, and the high-yield sugarcane planting technology is very necessary to be demonstrated and popularized in the Guangxi sugarcane planting area.|DISCLOSURE|Disclosure of Invention|[0011] The invention aims to provide a sugar cane high-yield planting method considering both carbon fixation and emission reduction of soil in a red soil area, which is a cultivation mode of 'interval local deep scarification and deep ploughing, uniform mixing of cane leaves and soil, deep planting, micro-cultivation for plant spacing, labor saving, fertilizer application and insect prevention for one time completion by using pesticide and fertilizer, high hilling and perennial root leveling and film covering', reduces the oil consumption of agricultural implement soil preparation and disturbance to soil, reduces organic carbon mineralization of soil, and reduces greenhouse gas emission; the problems that the conventional cultivated land is shallow in cultivation layer, large in intertillage and shallow in earthing up, and sugarcane falls down due to earthing up of a volcanic opening and the like are solved; the phenomenon that the straw piles influence the subsequent farming is reduced; labor cost for applying fertilizer and pesticide is reduced, and utilization rate of the fertilizer is improved; high hilling and perennial root flattening are combined, sugarcane is prevented from lodging, sugarcane bags are prevented from being rolled by a harvesting machine, high-position buds of perennial root sugarcane are prevented from early sprouting, the sugarcane yield is increased, and the perennial root sugarcane age is prolonged; finally achieving the purposes of carbon fixation and emission reduction of the soil of the sugarcane field, lodging resistance, and yield and efficiency increase of the sugarcane.|[0012] In order to realize the purpose of the invention, the technical scheme is as follows:|a high-yield planting method for sugar canes in a red soil area and with the functions of soil carbon sequestration and emission reduction is disclosed, which comprises the processes of sugarcane soil preparation, fertilization, seed arrangement, soil covering and film covering, ridging, weeding, harvesting, perennial root sugarcane leveling and film covering, and specifically comprises the following steps.|[0013] (1) Stubble cleaning and pre-ditching: and (3) crushing and stubble cleaning are carried out on the residues of the previous crops by adopting a stubble cleaning pre-furrowing machine, and meanwhile, linear pre-furrowing is carried out at a distance of 140cm, so as to linearly position the post-process.|[0014] (2) Local deep scarification and deep ploughing, ditching and base fertilizer application: adopting a tillage and soil preparation pipe all-in-one machine to carry out soil throwing type deep scarification and deep ploughing on broken soil in a ditch which is pre-opened, throwing the broken soil to two sides to form sugarcane planting ditches, wherein the width of each ditch is 70cm, two sides of each sugarcane planting ditch are not ploughed, and meanwhile, applying a special pesticide-fertilizer base fertilizer for sugarcane in the sugarcane planting ditches; the deep scarification, deep ploughing and soil breaking farming area occupies about one half of the original land, so that the oil consumption of agricultural implements and the disturbance to soil are reduced.|[0015] When the soil is crushed and thrown, the crushed soil and the broken straws of the previous stubbles are mixed uniformly, the problem that the straws are piled and erected in the empty soil when the common rotary cultivator works can be reduced, and the straw-stalk rotary cultivator can also be used for throwing the soilCan accelerate the decomposition of the straws and improve the organic matter content of the soil. The broken soil is thrown between the rows at two sides to form a concave groove with the planting depth being 20-25 cm lower than the original solid surface, the height from the bottom of the groove to the ridge surface being 50-60 cm, the width of the ridge surface being 50-60 cm and the width of the base of the ridge being 70cm, thus realizing deep planting of the sugarcane. For the lower part is real soil, the upper portion is for throwing the loose soil of going, and the maximum soaks the collection to concave type groove with natural precipitation like this, does benefit to soil and preserves water, and in the operation of ditching, the all-in-one is with fertilizer and the mixing of recess ditch soil, and fertilizer is only limited in recess ditch soil, realizes fertilizer deep fertilization, and recess ditch liquid manure coordinates, improves fertilizer utilization ratio, and sugarcane root system is perpendicular to prick anti lodging for the first time deeply. The base fertilizer is applied with the special pesticide fertilizer for the sugarcane, the fertilizer application and the pesticide application are carried out synchronously, the labor cost is reduced, and the application amount is N120 kg/hm2 、P2O5 80 kg/hm2 、K2O 150 kg/hm2The formula is suitable for the nutrient requirement of the sugarcane in the seedling stage, and the utilization rate of the fertilizer is improved. And the deep scarification, deep ploughing, ditching, soil throwing and fertilizing are completed by the all-in-one machine at one time, so that the labor efficiency is greatly improved.|[0016] (3) Seed arrangement, soil covering and film covering: carrying out automatic seed arrangement, soil covering and film covering planting by adopting a sugarcane planting machine, arranging two rows of sugarcane seeds in a sugarcane planting ditch, wherein the interval between the two rows of sugarcane seeds is 20 cm; the planter firstly loosens the soil on the two sides of the sugarcane seeds by unscrewing again to cover the soil on the sugarcane seeds. The covering soil for planting the sugarcane is thicker and about 9-11cm in autumn and winter, and is thinner and about 7-8cm in spring, so that early sprouting of the sugarcane seeds is facilitated. The degradable film with the width of 50 cm-60 cm is covered, when the film is pressed, the two sides of the mulching film are tightly pressed and tensioned, the film is not ventilated, the middle of the film is transparent for about 13-15cm, the water evaporation is prevented, the moisture is preserved, the temperature is kept, the sugarcane sprouts can be promoted only by water vapor below the ground without extra irrigation, the tensioned film is tightly attached to the ground, the sugarcane sprout top film breaking is facilitated, and the manual seedling picking operation cost is reduced. The sugarcane planter is purchased and used in the market or designed and used by the user.|[0017] (4) Fertilizing in seedling stage and physical weeding and micro-hilling: the sugarcane hiller is adopted, the seedling fertilizer N120 kg/hm2 is applied, the fertilizer is applied in combination, the sugarcane hiller carries out rotary tillage and soil throwing to turn the soil on the ridge surface to the ditch to cover 2-5 cm, micro-hilling is carried out, the phenomenon that large soil extrudes seedlings is avoided, the growing positions of the sugarcane seedlings can be scattered and positioned, the light transmittance and effective stems in the later period are increased, the moisture evaporation can be avoided, the sugarcane is promoted to root for the second time, row spacing weeds are rotated off in the rotary tillage and hilling process of the sugarcane hiller, and manual weeding and pesticide expenditure are reduced; the sugarcane banking machine is purchased or designed for use in the market.|[0018] (5) Fertilizing in the elongation period and high hilling: fertilizing and ridging operation is carried out by adopting the tillage and field management integrated machine in the step (2); applying sugarcane insecticide fertilizer, N260 kg/hm2、P2O5 40kg/hm2、K2O 150kg/hm2(ii) a The combined cutter rotating at high speed of the integrated tillage and soil preparation machine crushes soil on the ridge surface originally formed and then throws the crushed soil back to the base of the sugarcane plant, the ridging amount is 3 times of that of a conventional rotary cultivator, high ridging quality with full ridge shape, loose soil and complete and tight weed coverage is obtained, and the occurrence of 'fire hills' is reduced; after the hilling loose soil is solidified, the ridge height is 23-26cm, the sugarcane pocket is buried under the soil with the depth of 20-25 cm, the ridge surface width reaches 60-70 cm, and the ridge bottom width is 108-112cm, so that the lodging resistance of the sugarcane is improved, the crushing damage to the sugarcane pocket during mechanical harvesting is reduced, and the perennial root life is prolonged.|[0019] (6) Chemical weeding and harvesting: after the large hilling, the herbicide is sprayed in time for soil sealing, 55 to 70 percent of methyl, metolachlor, diuron 2700 and 3600g/hm2 are used for adding water 675L of weed stem leaves for directional spraying, or 200g/L of glufosinate ammonium 3000 and 4500 ml/hm2 Adding water 675L weed stem leaves, directionally spraying for 1 time, and preventing and treating for 12 times according to weed occurrence conditions at the later stage; the harvest can be carried out in the mature period of the sugarcane process.|[0020] (7) Leveling perennial root sugarcane and covering with a film: a ridge with the original height of 23-26cm of perennial root sugarcane is cut by a flattening machine with 13-16cm of sugarcane pocket, the ridge surface is smooth and convenient to cover with a film, soil on the ridge surface is thrown to the two outer sides of the sugarcane pocket, and the requirement of subsequent high hilling is met; after the ridge surface is leveled and reduced, the sugarcane is 10-12cm high in ridge, the perennial root sugarcane is covered with a film, water-retaining and heat-preserving, the germination of low-level buds is promoted, the emergence rate is improved, and the perennial root sugarcane age is prolonged; and (5) managing and harvesting according to the processes in the steps (4) to (6), wherein the perennial root sugarcanes adopt the processes until the sugarcane needs to be turned over again, and the sugarcane leaves are crushed and returned to the field after each batch of the sugarcane is harvested.|[0021] The integrated tillage and pipe-making machine is driven by a tractor in a traction way and comprises a rack and a gear box, wherein the gear box is arranged above the middle of the rack, power output shafts are respectively arranged at the left side and the right side of the gear box, and a power input main shaft which can be connected with a power shaft of the tractor is arranged at the front end of the gear box; the front end of the rack is provided with a side cantilever seat used for being connected with a side cantilever of a tractor in an installing way, and a middle cantilever seat used for being connected with a middle cantilever of the tractor in an installing way is arranged above the front end of the rack through a bracket; two sides of the lower part of the front end of the rack are respectively provided with a subsoiling plough through a subsoiling plough mounting seat, a gear transmission case is fixed on the rack right behind each subsoiling plough, the upper end of each gear transmission case is provided with a power input shaft, and the power input shaft is connected with a power output shaft through a coupling; two sides of the lower end of the gear transmission box are respectively provided with a driving shaft with the rotating direction opposite to the advancing direction of the integrated machine, and a plurality of rotary tillage soil throwing knives are arranged on the driving shaft through knife holders; a baffle is arranged at the lower part of the rack above the rotary tillage soil throwing cutter, one side of the baffle, which is far away from the gear transmission case, is hinged with a soil guide baffle through a hinge, the soil guide baffle is also connected with the rack through an angle adjusting rod, and the angle adjusting rod can adjust the opening angle of the soil guide baffle; the frame is provided with a fertilizing device which can automatically guide and convey fertilizer to the rear side of the gear transmission case.|[0022] Further preferably: fertilizing device include the fertilizer can, the fertilizer can passes through the fertilizer can rack-mount in the frame, install a motor gear case in the frame of fertilizer can lower part respectively, all be fixed with a lower fertile carousel that covers the fertilizer can play fertile mouthful in the pivot of motor gear case, the motor gear case utilizes the power drive of motor to descend fertile carousel rotatory, the outer wall of fertilizer can is provided with one and has the fertilizer scraping plate that is used for scraping the fertilizer in the fertile carousel down, scrape and install the lower fertile fill that is used for connecing the whereabouts fertilizer in the frame of fertilizer scraping plate below, the bottom intercommunication of lower fertile fill has the fertilizer guide pipe, the fertilizer guide pipe extends the rear side of gear drive case.|[0023] Further preferred is: the driving shaft is uniformly provided with three groups of rotary tillage soil throwing knives through the knife seats, each group of rotary tillage soil throwing knives consists of three rotary tillage soil throwing knives, and the three rotary tillage soil throwing knives are uniformly distributed on the knife seats, namely, are uniformly distributed on the circumference of the driving shaft.|[0024] Further preferred is: the rotary tillage soil throwing cutter comprises an L-shaped arc-shaped rotary tillage cutter and a soil throwing plate, a cutter handle is arranged at the straight end of the L-shaped arc-shaped rotary tillage cutter, a mounting hole for connecting and fixing the cutter handle with a cutter holder is formed in the cutter handle, the cutter handle is fixedly mounted with the cutter holder by adopting a bolt and a nut, and the soil throwing plate is fixed on the cambered surface of the uncut soil side of the arc-shaped end of the L-shaped arc-shaped rotary tillage cutter; the soil throwing plate and the knife face of the L-shaped arc rotary blade are arranged in an obtuse angle, and the angle of 120 plus 150 degrees is optimal. The soil throwing plate and the L-shaped arc rotary blade can also be integrally bent and formed.|[0025] Further preferred is: the deep scarification plough comprises a plough rod, a long tooth extending forwards is fixed on the front side of the bottom end of the plough rod, soil plowing plates inclining downwards from back to front are respectively arranged on the left side and the right side of the bottom end of the plough rod, and a short tooth extending forwards is fixed on the side, far away from the plough rod, of the front end of each soil plowing plate. Long tooth and short tooth correspond with the three groups of rotary tillage soil throwing knives of installation rear side, and long tooth and short tooth can be under the prerequisite that reduces the resistance as far as possible, plough the pine with earth, avoid the three groups of rotary tillage soil throwing knives of rear side can't realize local deep ploughing subsoiling hack.|[0026] Further preferred is: the left side and the right side of the plow lever above the soil plowing plate are respectively provided with a side plate which is opened backwards.|[0027] Further preferred is: the upper end of the plough rod is provided with a fixed mounting hole which is used for being fixedly connected with the deep scarification plough mounting seat.|[0028] The stubble cleaning pre-furrowing machine is driven by a tractor in a traction manner and comprises a machine frame I and a gear box I, wherein a side cantilever seat I used for being connected with a side cantilever of the tractor in an installation manner is arranged at the front end of the machine frame I, and a middle cantilever seat I used for being connected with a middle cantilever of the tractor in an installation manner is arranged above the front end of the machine frame I through a support I; the two sides of the front end of the machine frame I are respectively provided with a front scarification plough through scarification plough mounting seats, the distance between the two front scarification ploughs is determined according to the ditching planting row spacing, and the rear end machine frame I on the left side and the right side of each front scarification plough is respectively provided with a rear scarification plough through the scarification plough mounting seats; the rear end of the rack I is provided with a ditching plow frame, each ditching plow frame behind the front scarification plow is provided with a ditching and marking plow through a ditching plow mounting seat, the front scarification plow and the rear scarification plow carry out primary plow ditching, the farming resistance of the ditching and marking plow is reduced, the ditching and marking plow can plow deeper soil, and therefore the traction resistance of the whole combined machine is reduced; the gearbox I is arranged above the middle of the rack I, power output shafts I are respectively arranged on the left side and the right side of the gearbox I, and a power input main shaft I capable of being connected with a power shaft of a tractor is arranged at the front end of the gearbox I; the left side and the right side of the rack I are symmetrically and fixedly provided with a gear transmission case I, the upper end of the gear transmission case I is provided with a power input shaft I, and the power input shaft I is connected with a power output shaft I through a coupler I; a rotary tillage shaft is arranged between the lower ends of the two gear transmission boxes I through a bearing with a base, the rotary tillage shaft is connected with a gear in the gear transmission box I, and a stubble cleaning rotary blade is arranged on the rotary tillage shaft. According to production needs, the installation mode of the rear scarification plough, the ditching and scribing plough and the front scarification plough can be set to be in an up-and-down adjustable form, a plurality of adjusting holes can be formed in the plough rod, and the plurality of adjusting holes can be arranged to adjust the fixed positions of the plough rod seat and the plough rod so as to realize the height adjustment of the plough.|[0029] Further preferred is: the front end of the gear transmission case I is provided with a soil breaking plough, so that the gear transmission case I can cut into soil during tillage, and the stubble cleaning rotary blade can extend into the soil for tillage.|[0030] Further preferred is: frame I on install the baffle I that prevents earth and splash.|[0031] Further preferred is: the ditching plow frame is articulated to be installed in the rear end of frame I, the ditching plow frame still articulates with frame I or gear box I through hydraulic cylinder, hydraulic cylinder's jar seat is articulated with frame I or gear box I, hydraulic cylinder's piston rod is articulated with the ditching plow frame, through the upset of hydraulic cylinder control ditching plow frame, realize the control of the promotion of ditching marking plow and transferring.|[0032] The perennial root sugarcane is subjected to film covering, water retention and heat preservation, and a perennial root sugarcane root cutting, ridge breaking, fertilizing and film covering combined machine is adopted, is pulled by a tractor and comprises a rack III, wherein a side cantilever seat III used for being connected with a side cantilever of the tractor in an installing manner is arranged at the front end of the rack III, and a middle cantilever seat III used for being connected with a middle cantilever of the tractor in an installing manner is arranged above the front end of the rack III; a fertilizer box III is arranged on the rack III through a fertilizer box rack III, a gear box III driven by a hydraulic motor III is arranged on the rack III at the lower part of the fertilizer box III, and a lower fertilizer circular rotating disc III covering a fertilizer outlet at the bottom of the fertilizer box III is fixed on a rotating shaft of the gear box III; two sides of the outer wall of the fertilizer box III are respectively provided with a fertilizer scraping plate III for scraping the fertilizer in the lower fertilizer circular rotating disc III, two sides of the outer wall of the fertilizer box III are respectively provided with a lower fertilizer box III for receiving the falling fertilizer, and the bottom of the lower fertilizer box III is communicated with a fertilizer guide pipe III; two sides of the front end of the rack III are respectively provided with a root cutting and soil breaking rolling disc for cutting ridges and roots on two sides of a sugarcane ridge through rolling disc mounting seats, and the fertilizer guide pipe III extends to the rear outer side of the root cutting and soil breaking rolling disc; a film frame is arranged at the lower part of the rear end of the frame III, a film shaft for placing a mulching film is arranged on the film frame, and film pressing wheels for rolling two sides of the mulching film are arranged on the rear side of the film frame through wheel carriers; two sides of the rear end of the machine frame III are respectively provided with a hinge seat, two hinge seats are hinged with a mounting rod extending backwards, the bottom end of the mounting rod is connected with a tension spring connected with the bottom of the hinge seat, and the lower part of the rear end of the mounting rod is provided with a soil crushing and returning rolling disc used for scraping soil on two sides of a mulching film; the middle of the rear end of the rack III is connected with a support frame extending backwards, and two sides of the support frame are connected with mounting rods on two sides of the support frame through threaded adjusting connecting rods for limiting. The distance between the two soil crushing and returning rolling disks is larger than that between the two root cutting and soil breaking rolling disks, and the soil crushing and returning rolling disks crush soil and return to cover the two sides of the mulching film.|[0033] Further preferred is: the soil crushing and soil returning rolling disc comprises a rotating shaft seat and an installation rotating shaft, the installation rotating shaft is installed in the rotating shaft seat through a bearing, an arc-shaped soil returning circular disc is installed on the installation rotating shaft in a stretching mode, the top end of the rotating shaft seat is fixedly connected with a connecting shaft, a square shaft body and a threaded shaft body are arranged at the top end of the connecting shaft, and the threaded shaft body is located at the top of the square shaft body; the connecting axle passes through the axle sleeve to be connected with the installation pole, the vertical welded fastening of axle sleeve is at the end of installation pole, the upper end of axle sleeve is provided with the engaging lug, be provided with slot hole or a plurality of connecting hole on the engaging lug, the connecting axle passes and is equipped with the locking plate on the axle sleeve rear shape axle body, threaded shaft installs lock nut on one's body, be provided with the square hole that matches with square axle body on the locking plate, still be provided with the through-hole that corresponds with slot hole or connecting hole position on the engaging lug on the locking plate, the locking plate passes through the bolt and is connected with the engaging lug, through after unscrewing lock nut, the locking plate rotates, adjust the position of locking plate and engaging lug, realize the regulation of hack back soil rolling disc installation angle.|[0034] Further preferred is: the root cutting and soil breaking rolling disc comprises a root cutting rotating shaft and a rod seat, the root cutting rotating shaft is installed in the rod seat through a root cutting rotating shaft bearing, an arc root cutting disc is installed at the extending end of the root cutting rotating shaft, a rod seat installation plate used for being connected with the rolling disc installation seat through a bolt shaft is arranged at the top end of the arc root cutting disc through a connecting rod shaft, and the rod seat installation plate is located at the top of the connecting rod shaft. During installation, the arc-shaped surface of the arc-shaped root cutting disc is close to the perennial root sugarcane ridge, so that the problem that the sugarcane buds are broken due to the fact that soil is stirred towards the sugarcane when the arc-shaped root cutting disc cuts the root is avoided.|[0035] Further preferred is: the installation slot hole is formed in the rod seat installation plate, the installation position of the rolling disc installation seat is convenient to adjust due to the installation slot hole, and the installation angle of the root cutting and soil breaking rolling disc is achieved.|[0036] Further preferred is: arc hack dish's dish limit equipartition be provided with a plurality of soil cuts mouthful, the periphery is provided with a plurality of breachs promptly, can be better during the rotation smash earth and break ridge root cutting.|[0037] Further preferred is: the screw thread adjusting connecting rod comprises a connecting screw rod I, a screw rod connecting seat and a connecting screw rod II, the screw rod connecting seat is a hollow long connecting seat, the connecting screw rod I and the connecting screw rod II are respectively in threaded connection at two ends of the screw rod connecting seat, the connecting screw rod I is hinged to the mounting rod through a connecting lug ring, the connecting screw rod II is hinged to the supporting frame through the connecting lug ring, and a locking nut used for locking the connecting screw rod II and the screw rod connecting seat is installed on the connecting screw rod II.|[0038] Further preferred is: the middle part of lower fertile circle carousel III be provided with and avoid fertilizer to pile up the vertical circular cone housing at lower fertile circle carousel III middle part, the setting of circular cone housing will be followed the fertilizer that falls down in the fertilizer case III and led the periphery of delivering to fertile circle carousel III down.|[0039] Further preferred is: the conical housing is provided with a stirring blade for stirring fertilizer.|The sugar cane high-yield planting method considering both carbon fixation and emission reduction of the soil in the red soil area has the advantages that during the planting process, the local part of the sugar cane land is dug at intervals to reduce the soil disturbance, the disturbance of agricultural implements to the soil is reduced, and the greenhouse gas emission and the oil consumption of the agricultural implements are reduced; the sugarcane seeds are directly attached to the hard ground of the concave groove, and the method of promoting the germination of the sugarcane by using the ground gas is adopted; the soil crushing and throwing combined knife uniformly mixes the straws with soil, so that the problem that the stacking of the straws influences the subsequent farming is reduced, the decomposition of the straws is accelerated, and the organic matter content of the soil is improved; a planting method of deep planting of sugarcane, twice root-tying, high-cultivation lodging resistance, reduction of crater and prevention of rolling of a harvesting machine of a sugarcane pocket; a method for micro-hilling at the sugarcane seedling stage, fixing the growth position of the sugarcane seedlings, increasing the light transmittance and the number of effective stems at the later stage and physically weeding; the perennial root sugarcane is leveled and covered with a film, water retention and heat preservation are realized, the germination of low-position buds is promoted, the emergence rate is improved, and the age limit of the perennial root sugarcane is prolonged.|[0040] The planting method adopts the integrated machine of tillage, field preparation and management, which integrates the functions of deep tillage, deep scarification, ditching, soil breaking, fertilization, ridging and the like into a whole, has high working efficiency, and solves the problems that the traditional operation machine has single function and is not beneficial to the whole mechanized operation of sugarcane production; the rotary direction of the rotary tillage soil throwing cutter of the tillage and field management integrated machine is opposite to the advancing direction of the cultivator, the front part of the rotary tillage soil throwing cutter is provided with the deep scarification plough, the deep scarification plough and the deep scarification plough are matched to realize deep tillage and deep scarification, the key technology for realizing the difficult winding of weeds is realized, the continuous work of the cultivator is ensured, and the soil breaking and ridging operation is facilitated. And because the baffle and the soil guide baffle are arranged above the rotary tillage soil throwing knife, the broken soil thrown by the rotary tillage soil throwing knife can be guided to two sides by adjusting the opening angle of the soil guide baffle, the functions of ditching and earthing up can be realized, and the sugarcane buds cannot be extruded and damaged by throwing and earthing up, so that the earthing up effect is good. The fertilizer applying device guides the fertilizer to the rear side of the gear transmission box, and the rotary tillage soil throwing cutter rotates backwards to throw soil, so that the base fertilizer is positioned at the bottom of the sugarcane ditch, the base fertilizer drops to cover soil, the sugarcane seeds are separated from the base fertilizer, the phenomena of root burning and seed burning caused by fertilizer fermentation are avoided, and the germination rate and the survival rate of the sugarcane are improved. The subsoiling plough is provided with long teeth and short teeth which extend forwards, the long teeth and the short teeth correspond to three groups of rotary tillage soil throwing knives arranged on the rear side, the long teeth and the short teeth can loosen the soil plough on the premise of reducing resistance as much as possible, and the three groups of rotary tillage soil throwing knives on the rear side are favorable for realizing local subsoiling and soil crushing.|[0041] The stubble cleaning pre-ditching machine adopted by the planting method can complete stubble cleaning, local soil loosening and ditching at the same time, because the deep ditching planting can improve the drought resistance and lodging resistance of the sugarcane, and can also improve the yield of the sugarcane, but the one-time ditching planting of the tractor in the prior art can not meet the requirement, and the sugarcane field is reclaimed and reseeded, and the sugarcane field needs to be broken and returned to the field, stubble cleaning, soil loosening and ditching processes before reseeding and planting according to the agricultural production needs, the combined machine can loosen the soil, ditch and clear up the soil loosening, prepare for subsequent ditching and deep ditch planting, improve the walking route for the tractor, avoid the dragging of the deep ditching work by the subsequent tractor, improve the production efficiency and reduce the labor intensity; the front two sides of the front end of a frame I of the stubble ploughing pre-furrowing machine are respectively provided with a front scarification plough through a scarification plough mounting seat, the distance between the two front scarification ploughs is determined according to the row spacing of ditching planting, and the rear end frame I on the left side and the right side of each front scarification plough is respectively provided with a rear scarification plough through a scarification plough mounting seat; the rear end of the rack I is provided with a ditching plow frame, each ditching plow frame behind the front scarification plow is provided with a ditching and scribing plow through a ditching plow mounting seat, the matching mode of the front scarification plow and the two rear scarification plows is adopted for primary plowing and ditching, the farming resistance of the ditching and scribing plow is reduced, the ditching and scribing plow can plow deeper soil, and therefore the traction resistance of the whole combined machine is reduced; the front end of the gear transmission case I is provided with a soil breaking plough, so that the gear transmission case I can cut into soil during tillage, stubble cleaning rotary blades can extend into the soil for tillage, and thorough stubble cleaning is guaranteed.|[0042] The leveling machine adopted by the planting method can be used for downwards rotating and cutting the soil and the sugarcane heads of the upper stubble sugarcane ridges, the rotating and cutting depth is close to the height of the upper stubble sugarcane ridging, the limiting depth can be adjusted through the limiting wheel II, the soil leveling and cutting soil of the stubble cleaning rotary blade II is leveled by the soil leveling plough and is pushed towards sugarcane rows on two sides of the sugarcane ridges, so that enough soil is improved for the subsequent intertillage ridging, the growth of high-position buds is avoided, and the problem that the ratoon sugarcane ridging height is small because enough soil is not used for ridging during the intertillage ridging is avoided; the leveling machine can stir the crushed sugarcane leaves returned to the field and soil to return to the field, so that the sugarcane is decomposed into organic matters, and the sugarcane leaves returned to the field in the current year can provide nutrients for the growth of the sugarcane in the current year.|[0043] The perennial root sugarcane root cutting, ridge breaking, fertilizing and mulching combined machine adopted by the planting method can simultaneously cut roots, break ridges, fertilize and mulching on two sides of a perennial root sugarcane ridge, is high in working efficiency, and solves the problems of low germination rate, low tillering rate and low seedling rate of sugarcane high-position buds caused by the fact that a harvester and a conveyor are put into a field and rolled. The root cutting, ridge breaking, fertilization and film covering can be completed through one-time cultivation, fertilizers are accurately applied to the ridge sides of the sugarcanes, the mechanization degree of sugarcane planting management is improved, the yield per unit of the sugarcanes is improved, the perennial root age is prolonged, and the natural risk resistance is improved. The two sides of the front end of the frame III are respectively provided with a root cutting and soil breaking rolling disc through a root cutting and rolling disc mounting seat, the two root cutting and soil breaking rolling discs are used for cutting off lateral roots on two sides of a perennial root sugarcane ridge and turning over soil, the fertilizer guide pipe III applies fertilizer into the turned over soil, the arc-shaped surface of the arc root cutting disc is close to the perennial root sugarcane ridge, soil is turned over to the sugarcane when the arc root cutting disc is used for cutting the root, the sugarcane buds are pressed to be broken, and damage to soil loosening and fertilizing of the perennial root sugarcane can be reduced. Two sides of the rear end of the rack III are respectively provided with a hinge seat, two hinge seats are hinged with a mounting rod extending backwards, the bottom end of the mounting rod is connected with a tension spring connected with the bottom of the hinge seat, and the lower part of the rear end of the mounting rod is provided with a soil crushing and returning rolling disc used for scraping soil on two sides of a mulching film; the middle part of the rear end of the rack III is connected with a support frame extending backwards, and two sides of the support frame are respectively connected with mounting rods at two sides through a threaded adjusting connecting rod for limiting; the setting of structure like this can make the hack return soil rolling disc can paste tight ground all the time, can scrape the both sides of earth gland plastic film, guarantees that the plastic film both sides all have earth gland.|DRAWINGS DESCRIPTION|[0044] FIG. 1 is a schematic diagram of the structure of the integrated machine for tillage and soil preparation;|FIG. 2 is a schematic right-side view of FIG. 1;|FIG. 3 is a schematic structural view of a rotary tillage soil throwing blade;|FIG. 4 is a schematic top view of FIG. 3;|FIG. 5 is a schematic view of the construction of the subsoiler;|FIG. 6 is a schematic structural view of a stubble ploughing pre-furrowing machine adopted;|FIG. 7 is a schematic left side view of FIG. 6;|FIG. 8 is a top schematic view of FIG. 6;|FIG. 9 is a schematic structural view of a root-cutting, ridge-breaking, fertilizing and film-covering combined machine for perennial sugarcane;|FIG. 10 is a schematic left side view of FIG. 9;|FIG. 11 is a schematic top view of FIG. 9;|FIG. 12 is a schematic structural view of a root cutting and soil breaking rolling disc;|FIG. 13 is a schematic view taken from the direction A-A of FIG. 12;|FIG. 14 is a top schematic view of FIG. 12;|FIG. 15 is a schematic structural view of a soil crushing and returning rolling disc;|FIG. 16 is a schematic view of the mounting structure of the lower spheroidicity rotary table III;|FIG. 17 is a top schematic view of FIG. 16;|FIG. 18 is a schematic view of a threaded adjusting connecting rod;|the part names of the sequence numbers in the figure are:|1. a frame, 2, a fertilizer box frame, 3, a fertilizer guide pipe, 4, a fertilizer discharging bucket, 5, a motor gear box, 6, a fertilizer scraping plate, 7, a fertilizer discharging turntable, 8, a fertilizer box, 9, a middle cantilever seat, 10, a bracket, 11, a gear box, 12, a power input main shaft, 13, a power input shaft, 14, a gear transmission box, 15, a side cantilever seat, 16, a deep loosening plough mounting seat, 17, a deep loosening plough, 18, a rotary tillage soil throwing knife, 19, a knife seat, 20, a driving shaft, 21, a soil guide baffle, 22, a baffle, 23, a hinge, 24, an angle adjusting rod, 25, a power output shaft, 26, a coupler, 27, an L-shaped arc rotary tillage knife, 28, a soil throwing plate, 29, a knife handle, 30, a mounting hole, 31, a short tooth, 32, a soil throwing plate, 33, a side plate, 34, a plough rod, 35, a fixed mounting hole, 36, a long tooth, 37, a broken soil, 38, a gear transmission box I, 39 and a bearing with a seat, 40. rotary tillage shaft, 41, stubble ploughing rotary blade, 42, machine frame I, 43, baffle I, 44, power input shaft I, 45, coupling I, 46, side cantilever base I, 47, power output shaft I, 48, gear box I, 49, power input main shaft I, 50, middle cantilever base I, 51, support I, 52, rear scarification plough, 53, ditching and marking plough, 54, front scarification plough, 55, scarification plough mounting base, 56, ditching mounting base, 57, ditching plough frame, 58, hydraulic cylinder, 59, root cutting and breaking rolling disc, 60, side cantilever base III, 61, machine frame III, 62, rolling disc mounting base, 63, hydraulic motor III, 64, gear box III, 65, middle cantilever base III, 66, fertilizer box frame III, 67, fertilizer box III, 68, fertilizer scraping plate III, 69, fertilizer circular fertilizer rotating disc, 70, fertilizer bucket, 71, hinged base, 72, tension spring, 73, threaded connecting rod, 74. the soil back-grinding device comprises a support frame, 75, an installation rod, 76, a locking plate, 77, a soil back-grinding rolling disc, 78, a film pressing wheel, 79, a wheel frame, 80, a film shaft, 81, a film frame, 82, a fertilizer guide pipe III, 83, a conical housing, 84, a toggle blade, 85, a root cutting rotating shaft, 86, a root cutting rotating shaft bearing, 87, a rod seat, 88, a rod seat installation plate, 89, an installation long hole, 90, an arc root cutting disc, 91, a soil cutting opening, 92, a rotating shaft seat, 93, a connecting shaft, 94, a square shaft body, 95, a threaded shaft body, 96, an arc soil back-grinding disc, 97, an installation rotating shaft, 98, a connecting screw rod I, 99, a screw rod connection seat, 100, a locking nut, 101 and a connecting screw rod II.|INVENTION MODE|Detailed Description|[0045] The present application will be described in further detail with reference to the accompanying drawings and examples.|[0046] Example 1|The sugar cane high-yield planting method can realize the high-yield planting of the sugar cane in the red soil area with the functions of carbon sequestration and emission reduction of the soil by adopting the following steps:|(1) stubble cleaning and pre-ditching: and (3) crushing and stubble cleaning are carried out on the residues of the previous crops by adopting a stubble cleaning pre-furrowing machine, and meanwhile, linear pre-furrowing is carried out at a distance of 140cm, so as to linearly position the post-process.|[0047] (2) Local deep scarification and deep ploughing, ditching and base fertilizer application: adopting a tillage and soil preparation pipe all-in-one machine to carry out soil throwing type deep scarification and deep ploughing on broken soil in a ditch which is pre-opened, throwing the broken soil to two sides to form sugarcane planting ditches, wherein the width of each ditch is 70cm, two sides of each sugarcane planting ditch are not ploughed, and meanwhile, applying a special pesticide-fertilizer base fertilizer for sugarcane in the sugarcane planting ditches; the deep scarification, deep ploughing and soil breaking farming area occupies about one half of the original land, so that the oil consumption of agricultural implements and the disturbance to soil are reduced.|[0048] When the soil is crushed and thrown, the crushed soil and the broken straws of the previous stubbles are uniformly mixed, so that the problem of the straw pile-up and empty soil during the operation of the common rotary cultivator can be solved, the decomposition of the straws can be accelerated, and the organic matter content of the soil can be improved. The broken soil is thrown between the rows at two sides to form a concave groove with the planting depth being 20-25 cm lower than the original solid surface, the height from the bottom of the groove to the ridge surface being 50-60 cm, the width of the ridge surface being 50-60 cm and the width of the base of the ridge being 70cm, thus realizing deep planting of the sugarcane. For the lower part is real soil, the upper portion is for throwing the loose soil of going, and the maximum soaks the collection to concave type groove with natural precipitation like this, does benefit to soil and preserves water, and in the operation of ditching, the all-in-one is with fertilizer and the mixing of recess ditch soil, and fertilizer is only limited in recess ditch soil, realizes fertilizer deep fertilization, and recess ditch liquid manure coordinates, improves fertilizer utilization ratio, and sugarcane root system is perpendicular to prick anti lodging for the first time deeply. The base fertilizer is applied with the special pesticide fertilizer for the sugarcane, the fertilizer application and the pesticide application are carried out synchronously, the labor cost is reduced, and the application amount is N120 kg/hm2 、P2O5 80 kg/hm2 、K2O 150 kg/hm2The formula is suitable for the nutrient requirement of the sugarcane in the seedling stage, and the utilization rate of the fertilizer is improved. And the deep scarification, deep ploughing, ditching, soil throwing and fertilizing are completed by the all-in-one machine at one time, so that the labor efficiency is greatly improved.|[0049] (3) Seed arrangement, soil covering and film covering: carrying out automatic seed arrangement, soil covering and film covering planting by adopting a sugarcane planting machine, arranging two rows of sugarcane seeds in a sugarcane planting ditch, wherein the interval between the two rows of sugarcane seeds is 20 cm; the planter firstly loosens the soil on the two sides of the sugarcane seeds by unscrewing again to cover the soil on the sugarcane seeds. The covering soil for planting the sugarcane is thicker and about 9-11cm in autumn and winter, and is thinner and about 7-8cm in spring, so that early sprouting of the sugarcane seeds is facilitated. The degradable film with the width of 50 cm-60 cm is covered, when the film is pressed, the two sides of the mulching film are tightly pressed and tensioned, the film is not ventilated, the middle of the film is transparent for about 13-15cm, the water evaporation is prevented, the moisture is preserved, the temperature is kept, the sugarcane sprouts can be promoted only by water vapor below the ground without extra irrigation, the tensioned film is tightly attached to the ground, the sugarcane sprout top film breaking is facilitated, and the manual seedling picking operation cost is reduced. The sugarcane planter is purchased and used in the market or designed and used by the user.|[0050] (4) Fertilizing in seedling stage and physical weeding and micro-hilling: the sugarcane hiller is adopted, the seedling fertilizer N120 kg/hm2 is applied, the fertilizer is applied in combination, the sugarcane hiller carries out rotary tillage and soil throwing to turn the soil on the ridge surface to the ditch to cover 2-5 cm, micro-hilling is carried out, the phenomenon that large soil extrudes seedlings is avoided, the growing positions of the sugarcane seedlings can be scattered and positioned, the light transmittance and effective stems in the later period are increased, the moisture evaporation can be avoided, the sugarcane is promoted to root for the second time, row spacing weeds are rotated off in the rotary tillage and hilling process of the sugarcane hiller, and manual weeding and pesticide expenditure are reduced; the sugarcane banking machine is purchased or designed for use in the market.|[0051] (5) Fertilizing in the elongation period and high hilling: fertilizing and ridging operation is carried out by adopting the tillage and field management integrated machine in the step (2); applying sugarcane insecticide fertilizer, N260 kg/hm2、P2O5 40kg/hm2、K2O 150kg/hm2(ii) a The combined cutter rotating at high speed of the integrated tillage and soil preparation machine crushes soil on the ridge surface originally formed and then throws the crushed soil back to the base of the sugarcane plant, the ridging amount is 3 times of that of a conventional rotary cultivator, high ridging quality with full ridge shape, loose soil and complete and tight weed coverage is obtained, and the occurrence of 'fire hills' is reduced; after the hilling loose soil is solidified, the ridge height is 23-26cm, the sugarcane pocket is buried under the soil with the depth of 20-25 cm, the ridge surface width reaches 60-70 cm, and the ridge bottom width is 108-112cm, so that the lodging resistance of the sugarcane is improved, the crushing damage to the sugarcane pocket during mechanical harvesting is reduced, and the perennial root life is prolonged.|[0052] (6) Chemical weeding and harvesting: after the large hilling, the herbicide is sprayed in time for soil sealing, 55 to 70 percent of methyl, metolachlor, diuron 2700 and 3600g/hm2 are used for adding water 675L of weed stem leaves for directional spraying, or 200g/L of glufosinate ammonium 3000 and 4500 ml/hm2 Adding water 675L weed stem leaves, directionally spraying for 1 time, and preventing and treating for 12 times according to weed occurrence conditions at the later stage; the harvest can be carried out in the mature period of the sugarcane process.|[0053] (7) Leveling perennial root sugarcane and covering with a film: a ridge with the original height of 23-26cm of perennial root sugarcane is cut by a flattening machine with 13-16cm of sugarcane pocket, the ridge surface is smooth and convenient to cover with a film, soil on the ridge surface is thrown to the two outer sides of the sugarcane pocket, and the requirement of subsequent high hilling is met; after the ridge surface is leveled and reduced, the sugarcane is 10-12cm high in ridge, the perennial root sugarcane is covered with a film, water-retaining and heat-preserving, the germination of low-level buds is promoted, the emergence rate is improved, and the perennial root sugarcane age is prolonged; and (5) managing and harvesting according to the processes in the steps (4) to (6), wherein the perennial root sugarcanes adopt the processes until the sugarcane needs to be turned over again, and the sugarcane leaves are crushed and returned to the field after each batch of the sugarcane is harvested.|[0054] The integrated tillage and pipe-making machine is driven by a tractor in a traction way and comprises a rack 1 and a gear box 11, wherein the gear box 11 is arranged above the middle of the rack 1, the left side and the right side of the gear box 11 are respectively provided with a power output shaft 25, and the front end of the gear box 11 is provided with a power input main shaft 12 which can be connected with the power shaft of the tractor; a side cantilever seat 15 used for being connected with a side cantilever of a tractor in an installing way is arranged at the front end of the frame 1, and a middle cantilever seat 9 used for being connected with a middle cantilever of the tractor in an installing way is arranged above the front end of the frame 1 through a support 10; the deep loosening plough 17 is mounted on two sides of the lower portion of the front end of the frame 1 through deep loosening plough mounting seats 16 respectively, the deep loosening plough 17 comprises a plough rod 34, a long tooth 36 extending forwards is fixed on the front side of the bottom end of the plough rod 34, soil plowing plates 32 inclining downwards from back to front are arranged on the left side and the right side of the bottom end of the plough rod 34 respectively, and a short tooth 31 extending forwards is fixed on the side, far away from the plough rod 34, of the front ends of the soil plowing plates 32. The left side and the right side of a plow rod 34 above the soil plowing plate 32 are respectively provided with a side plate 33 which is opened backwards. The upper end of the plow lever 34 is provided with a fixed mounting hole 35 for connecting and fixing with the deep loosening plow mounting base 16. A gear transmission case 14 is fixed on the frame 1 right behind each subsoiling plough 17, a power input shaft 13 is mounted at the upper end of the gear transmission case 14, and the power input shaft 13 is connected with a power output shaft 25 through a coupling 26; two sides of the lower end of the gear transmission box 14 are respectively provided with a driving shaft 20 with the rotation direction opposite to the advancing direction of the all-in-one machine, three groups of rotary tillage soil throwing knives 18 are uniformly distributed on each driving shaft 20 through a knife seat 19, and the three groups of rotary tillage soil throwing knives 18 respectively correspond to one knife seat 19; each group of rotary tillage soil throwing blades 18 consists of three rotary tillage soil throwing blades 18, and the three rotary tillage soil throwing blades 18 are uniformly distributed on a blade holder 19, namely on the circumference of a driving shaft 20. The rotary tillage soil throwing blade 18 comprises an L-shaped arc rotary tillage blade 27 and a soil throwing plate 28, a knife handle 29 is arranged at the straight end of the L-shaped arc rotary tillage blade 27, a mounting hole 30 for connecting and fixing the knife handle 29 with the knife holder 19 is formed in the knife handle 29, and the soil throwing plate 28 is fixed on the arc surface of the non-soil cutting side of the arc end of the L-shaped arc rotary tillage blade 27; the soil throwing plate 28 and the blade face of the L-shaped arc rotary blade 27 are arranged in an obtuse angle. The soil throwing plate 28 and the L-shaped arc rotary blade 27 can also be integrally formed by bending. A baffle 22 is arranged at the lower part of the frame 1 above the rotary tillage soil throwing knife 18, one side of the baffle 22 far away from the gear transmission case 14 is hinged with a soil guiding baffle 21 through a hinge 23, the soil guiding baffle 21 is also connected with the frame 1 through an angle adjusting rod 24, and the angle adjusting rod 24 can adjust the opening angle of the soil guiding baffle 21; a fertilizing device which can automatically guide fertilizer to the rear side of the gear transmission case 14 is arranged on the frame 1; fertilizer injection unit include fertilizer box 8, fertilizer box 8 passes through fertilizer box frame 2 and installs in frame 1, install a motor gear box 5 on the frame 1 of 8 lower parts of fertilizer box respectively, all be fixed with a lower fertilizer carousel 7 that covers 8 fertilizer outlets of fertilizer box in the pivot of motor gear box 5, motor gear box 5 utilizes the power drive of motor to descend fertilizer carousel 7 rotatory, fertilizer box 8's outer wall is provided with one and is used for scraping the fertilizer in lower fertilizer carousel 7 and scrapes fertilizer board 6, scrape and install the lower fertilizer fill 4 that is used for connecing the whereabouts fertilizer on the frame 1 of fertilizer board 6 below, the bottom intercommunication of lower fertilizer fill 4 has fertilizer guide 3, fertilizer guide 3 extends gear drive case 14 rear side.|[0055] The working principle of the adopted tillage and soil preparation pipe all-in-one machine is as follows: the side cantilever and the side cantilever seat 15 of the tractor are connected in an installing way, the middle cantilever and the middle cantilever seat 9 of the tractor are connected in an installing way, and the side cantilever and the middle cantilever of the tractor are used for controlling the lifting and lowering of the tillage and soil preparation pipe all-in-one machine. When the cultivator is not used for cultivating, the cultivator-pipe integrated machine is lifted by the side cantilever and the middle cantilever of the tractor. When the sugarcane is planted, the tractor puts the tillage and soil preparation pipe all-in-one machine down, fertilizer is put into the fertilizer box 8, the tractor is driven to travel by traction, the motor gear box 5 drives the fertilizer-discharging rotary disc 7 to rotate by the power of the motor, and the deep scarification plough 17 cuts and digs soil, so that the working resistance of the rotary tillage soil-throwing knife 18 arranged at the rear side can be reduced, and the local deep tillage and deep scarification of the rotary tillage soil-throwing knife 18 are facilitated; the power output by the tractor is transmitted into the gear box 11 from the power input main shaft 12, the power is respectively transmitted to the power input shaft 13 from the power output shafts 25 at two sides of the gear box 11 through the shaft couplings 26, the power is transmitted into the gear transmission box 14, the driving shaft 20 is driven to drive the rotary tillage soil throwing cutter 18 to rotate backwards to break soil and throw soil through the action of the soil guide baffle plate 21 and the baffle plate 22, soil is turned and thrown towards two sides to form a sugarcane planting ditch, the fertilizer in the fertilizer box 8 falls onto the lower fertilizer rotating disc 7, the fertilizer in the lower fertilizer rotating disc 7 is scraped into the lower fertilizer bucket 4 due to the rotation of the lower fertilizer rotating disc 7 and the blocking action of the fertilizer scraping plate 6, the fertilizer is discharged into the sugarcane planting ditch through the action of the fertilizer guide pipe 3, a small part of broken soil falls into the ditch during the working process of the rotary tillage soil throwing cutter to cover the fertilizer, and the fertilizer is separated from the sugarcane when the sugarcane seeds fall into the ditch, avoids the phenomena of root burning and seed burning caused by fertilizer fermentation, and improves the germination rate and the survival rate of the sugarcane. When the soil is required to be hilled, the fertilizer applying device is stopped to work, and the opening angle of the soil guide baffle 21 is adjusted to enable soil to be turned over towards the root of the sugarcane ridge.|[0056] The stubble-cleaning pre-furrowing machine is driven by a tractor in a traction manner and comprises a machine frame I42 and a gear box I48, wherein a side cantilever seat I46 used for being connected with a side cantilever of the tractor in an installation manner is arranged at the front end of the machine frame I42, and a middle cantilever seat I50 used for being connected with a middle cantilever of the tractor in an installation manner is arranged above the front end of the machine frame I42 through a support I51; the two sides of the front end of the frame I42 are respectively provided with a front scarification plough 54 through a scarification plough mounting seat 55, the distance between the two front scarification ploughs 54 is determined according to the row spacing of ditching and planting, and the rear end frame I42 at the left side and the right side of each front scarification plough 54 is respectively provided with a rear scarification plough 52 through the scarification plough mounting seat 55; the ditching plow frame 57 is hinged to the rear end of the machine frame I42, a ditching and marking plow 53 is mounted on the ditching plow frame 57 behind each front scarification plow 54 through a ditching plow mounting seat 56, the front scarification plow 54 and the rear scarification plow 52 carry out primary plow ditching, the farming resistance of the ditching and marking plow 53 is reduced, the ditching and marking plow 53 can plow deeper soil, and the traction resistance of the whole combined machine is reduced; the ditching plow frame 57 is also hinged with the machine frame I42 or the gear box I48 through a hydraulic oil cylinder 58, a cylinder seat of the hydraulic oil cylinder 58 is hinged with the machine frame I42 or the gear box I48, a piston rod of the hydraulic oil cylinder 58 is hinged with the ditching plow frame 57, the ditching plow frame 57 is controlled to turn through the hydraulic oil cylinder 58, and the control of lifting and lowering of the ditching marking plow 53 is realized. A baffle I43 for preventing mud from splashing is mounted on the machine frame I42. The gearbox I48 is arranged above the middle of the rack I42, power output shafts I47 are respectively arranged on the left side and the right side of the gearbox I48, and a power input main shaft I49 capable of being connected with a power shaft of a tractor is arranged at the front end of the gearbox I48; the left side and the right side of the rack I42 are symmetrically and fixedly provided with a gear transmission box I38, the upper end of the gear transmission box I38 is provided with a power input shaft I44, and the power input shaft I44 is connected with a power output shaft I47 through a coupler I45; a rotary tillage shaft 40 is arranged between the lower ends of the two gear transmission boxes I38 through a bearing 39 with a base, the rotary tillage shaft 40 is connected with a gear in the gear transmission box I38, and a stubble cleaning rotary blade 41 is arranged on the rotary tillage shaft 40. The front end of the gear transmission box I38 is provided with a soil breaking plough 37, so that the gear transmission box I38 can cut into soil during tillage, and the stubble cleaning rotary blade 41 can extend into the soil for tillage.|[0057] The working principle of the stubble-cleaning pre-furrowing machine is as follows: the side cantilever of a tractor is connected with a side cantilever seat I46 in an installing way, the middle cantilever of the tractor is connected with a middle cantilever seat I50 in an installing way, a power shaft at the rear end of the tractor is connected with a power input main shaft I49, and the tractor controls the combination machine to ascend and descend; hydraulic rams 58 are connected to a hydraulic cylinder control system. When the combined machine is not used for tillage during walking, the combined machine is lifted through the side cantilever and the middle cantilever of the tractor, and the ditching plow frame 57 is turned upwards by the hydraulic oil cylinder 58. When the land needs to be cultivated, the tractor lowers the combined machine and drives the combined machine to walk, the power output by the tractor is transmitted into the gear box I48 from the power input main shaft I49, the power is respectively transmitted to the power input shaft I44 from the power output shafts I47 at the two sides of the gear box I48 through the shaft coupling I45, the power is transmitted into the gear transmission box I38 of the frame I42, the rotary tillage shaft 40 is driven to drive the stubble-cleaning rotary blade 41 to rotate and clean the stubble after being transmitted by the gears in the gear transmission box I38, the soil breaking plough 37 at the front end of the gear transmission box I38 breaks the soil, the gear transmission case I38 is enabled to cut into soil, the front scarification plough 54 and the rear scarification plough 52 carry out primary plough ditching, the farming resistance of the ditching and marking plough 53 is reduced, the hydraulic oil cylinder 58 turns the ditching plough frame 57 downwards, the ditching and marking plough 53 ploughs into the soil, ditching and soil loosening are cleaned, preparation is made for subsequent ditching and deep groove planting, the walking route is also improved for the tractor, and the tractor is prevented from working and slipping. The pre-ditching can pull loose soil open, when the following tractor pulls the deep ditching, the tractor runs and skids, if the pre-ditching is not carried out, when the tractor pulls the deep ditching, the tractor wheel is easy to skid, and the deep ditching can be realized very much.|[0058] The perennial root sugarcane is subjected to film covering, water retention and heat preservation, and a perennial root sugarcane root cutting, ridge breaking, fertilizing and film covering combined machine is adopted and comprises a rack III 89, the front end of the rack III 89 is provided with a side cantilever seat III 88 for being connected with a side cantilever of a tractor in an installing manner, and a middle cantilever seat III 93 for being connected with a middle cantilever of the tractor in an installing manner is arranged above the front end of the rack III 89; a fertilizer box III 95 is arranged on the rack III 89 through a fertilizer box rack III 94, a gear box III 92 driven by a hydraulic motor III 91 is arranged on the rack III 89 at the lower part of the fertilizer box III 95, and a lower fertilizer circular rotating disc III 97 covering a fertilizer outlet at the bottom of the fertilizer box III 95 is fixed on a rotating shaft of the gear box III 92; two sides of the outer wall of the fertilizer box III 95 are respectively provided with a fertilizer scraping plate III 96 used for scraping the fertilizer in the lower fertilizer circular turntable III 97, two sides of the outer wall of the fertilizer box III 95 are respectively provided with a lower fertilizer bucket III 98 used for receiving the falling fertilizer, and the bottom of the lower fertilizer bucket III 98 is communicated with a fertilizer guide pipe III 110; two sides of the front end of the rack III 89 are respectively provided with a root cutting and soil breaking rolling disc 87 for breaking ridges and cutting roots on two sides of a sugarcane ridge through rolling disc mounting seats 90, and the fertilizer guide pipe III 110 extends to the rear outer side of the root cutting and soil breaking rolling disc 87; a film frame 109 is arranged at the lower part of the rear end of the rack III 89, a film shaft 108 for placing a mulching film is arranged on the film frame 109, and a film pressing wheel 106 for rolling the two sides of the mulching film is arranged at the rear side of the film frame 109 through a wheel carrier 107; two sides of the rear end of the rack III 89 are respectively provided with a hinge seat 99, two hinge seats 99 are hinged with a mounting rod 103 extending backwards, the bottom end of the mounting rod 103 is connected with a tension spring 100 connected with the bottom of the hinge seat 99, and the lower part of the rear end of the mounting rod 103 is provided with a soil crushing and returning rolling disc 105 used for scraping soil on two sides of a mulching film; the middle part of the rear end of the rack III 89 is connected with a support frame 102 extending backwards, and two sides of the support frame 102 are respectively connected with mounting rods 103 at two sides through a threaded adjusting connecting rod 101 for limiting. The distance between the two soil breaking and returning rolling disks 105 is larger than the distance between the two root cutting and soil breaking rolling disks 87. The soil crushing and soil returning rolling disc 105 comprises a rotating shaft seat 120 and an installation rotating shaft 125, the installation rotating shaft 125 is installed in the rotating shaft seat 120 through a bearing, an arc-shaped soil returning circular disc 124 is installed on the installation rotating shaft 125 in a stretching mode, the top end of the rotating shaft seat 120 is fixedly connected with a connecting shaft 121, a square shaft body 122 and a threaded shaft body 123 are arranged at the top end of the connecting shaft 121, and the threaded shaft body 123 is located at the top of the square shaft body 122; connecting axle 121 passes through the axle sleeve and is connected with installation pole 103, the vertical welded fastening of axle sleeve is at the end of installation pole 103, the upper end of axle sleeve is provided with the engaging lug, be provided with slot hole or a plurality of connecting hole on the engaging lug, connecting axle 121 is equipped with locking plate 104 on passing square axle body 122 behind the axle sleeve, install lock nut on the screw thread axle body 123, be provided with the square hole that matches with square axle body 122 on the locking plate 104, still be provided with the through-hole that corresponds with slot hole or connecting hole position on the engaging lug on the locking plate 104, locking plate 104 passes through the bolt and is connected with the engaging lug, through unscrewing the lock nut after, lock plate 104 rotates, adjust the position of locking plate 104 and engaging lug, realize the regulation of hack return native rolling disc 105 installation angle. The root cutting and soil breaking rolling disc 87 comprises a root cutting rotating shaft 113 and a rod seat 115, the root cutting rotating shaft 113 is installed in the rod seat 115 through a root cutting rotating shaft bearing 114, an arc-shaped root cutting disc 118 is installed at the extending end of the root cutting rotating shaft 113, the top end of the arc-shaped root cutting disc 118 is provided with a rod seat installation plate 116 which is connected with the rolling disc installation seat 90 through bolts through a connecting rod shaft, and the rod seat installation plate 116 is located at the top of the connecting rod shaft. The rod seat mounting plate 116 is provided with a mounting long hole 117, the mounting position of the rolling disc mounting seat 90 can be conveniently adjusted by the mounting long hole 117, and the mounting angle of the root cutting and soil breaking rolling disc 87 is realized. The plate edge of the arc soil crushing plate 23 is uniformly provided with a plurality of soil cutting openings 119. The thread adjusting connecting rod 101 comprises a connecting screw I126, a screw connecting seat 127 and a connecting screw II 129, the screw connecting seat 127 is a hollow long connecting seat, the connecting screw I126 and the connecting screw II 129 are respectively in threaded connection with two ends of the screw connecting seat 127, the connecting screw I126 is hinged to the mounting rod 103 through a connecting lug ring, the connecting screw II 129 is hinged to the supporting frame 102 through the connecting lug ring, and a locking nut 128 used for locking the connecting screw II 129 and the screw connecting seat 127 is mounted on the connecting screw II 129. The middle part of lower fertile circle carousel III 97 be provided with and avoid fertilizer to pile up the vertical circular cone housing 111 in lower fertile circle carousel III 97 middle part, the setting of circular cone housing 111 will be from the fertilizer that falls in the fertile case III 95 lead the periphery of delivering to fertile circle carousel III 97 down. The conical housing 111 is provided with a stirring blade 112 for stirring fertilizer.|[0059] The operating principle of the perennial sugarcane root cutting, ridge breaking, fertilizing and film covering combined machine is as follows: the side cantilever and the side cantilever seat III 88 of the tractor are connected in an installing mode, the middle cantilever and the middle cantilever seat III 93 of the tractor are connected in an installing mode, and the side cantilever and the middle cantilever of the tractor are used for controlling the rising and the lowering of the perennial sugarcane root cutting, ridge breaking, fertilizing and mulching combined machine. According to the actual ridge width of the perennial root sugarcane, the distance between the two root cutting and soil breaking rolling discs 87 is adjusted by adjusting the installation positions of the rolling disc installation seats 90, and the distance between the two installation rods 103 is adjusted by adjusting the installation positions of the hinged seats 99, so that the distance between the soil breaking and soil returning rolling discs 105 is adjusted;|when the sugarcane harvester is not used for farming during walking, the perennial sugarcane root cutting, ridge breaking, fertilizing and mulching combined machine is lifted through the side cantilever and the middle cantilever of the tractor. When the land needs to be cultivated, a tractor lowers a ratoon sugarcane root cutting, ridge breaking, fertilizing and mulching combined machine, two root cutting, soil breaking and rolling disks 87 are positioned on two sides of a sugarcane ridge, fertilizer is put into a fertilizer box III 95, a mulching film roll is collided on a film shaft 108, a film pressing wheel 106 is favorable for pressing two sides of a mulching film, the tractor drives the sugarcane to travel, meanwhile, a hydraulic motor III 91 drives a lower fertilizer circle rotating disk III 97 to rotate through a gear box III 92, and the two root cutting, soil breaking and rolling disks 87 cut off and turn over soil on the side roots on the two sides of the ratoon sugarcane ridge; the fertilizer in the fertilizer box III 95 falls on the lower fertilizer circular turntable III 97, the fertilizer in the lower fertilizer circular turntable III 97 is scraped to fall into the lower fertilizer bucket III 98 due to the rotation of the lower fertilizer circular turntable III 97 and the blocking action of the fertilizer scraping plate III 96, the fertilizer is discharged to the lower part of soil stirred by the root cutting and soil breaking rolling disc 87 under the action of the fertilizer guide pipe III 110, the soil breaking and soil returning rolling disc 105 is dragged at the rear side to cut and break the soil, the mulching is finished by guiding the two sides of the mulching film to be covered, the root cutting and ridge breaking, the fertilization and the mulching of the perennial sugarcane can be finished by one-time operation, and the sprouting and the growth of the perennial sugarcane are facilitated.|[0060] Application case|The high-yield planting method for sugar cane carries out test demonstration in the town of Wuming Altar at 2020, 1 month to 2021, 12 months, designs two treatments of conventional cultivation of farmers and cultivation of the invention, and each treated land is 666.6m2This was repeated three times. The high-yield planting method of the sugar cane comprises the following specific steps:|1. in 1 month, 120 horsepower rotary cultivator equipped with Beidou navigation system is adopted, the residue of the previous crop is crushed and stubble-cleaned, and meanwhile, the straight line with the distance of 140cm is pre-ditched. 2. Adopting a deep scarification and deep ploughing, soil crushing, soil throwing, ditching and fertilizing all-in-one machine, locally and deeply ploughing, soil crushing and throwing and ditching, throwing soil into the space between two side rows to form a planting ditch with the depth being 20 cm-25 cm lower than the original field surface, forming a concave groove below the ground solid soil, the height from the ditch bottom to the ridge surface being 50 cm-60 cm, the width of the ridge surface being 50 cm-60 cm and the width of the ridge base being 70cm, applying base fertilizer while ditching, applying 750 kg/hm of sugarcane pesticide fertilizer containing 0.05 percent of dinotefuran2. 3. Seed arrangement, soil covering and film covering are carried out by adopting a sugarcane split type planter, the sugarcane is planted in a double-row manner of willow city 05/136, the spacing between two rows of sugarcane seeds is about 20cm, and the seeding amount is 10.5 t/hm2. 4. Applying 250 kg/hm of urea to the sugarcane banking machine in the seedling stage of the sugarcane in the middle ten days of the 4 th month2And at the same time of fertilizing, the grass is removed by a physical method. 5. In the elongation period of the sugarcane in the last 6 months, a deep-scarification, deep-ploughing, soil-breaking, furrowing and fertilization all-in-one machine is adopted for fertilizing and hilling, and 100 kg/hm of sugarcane pesticide fertilizer containing 0.05 percent of dinotefuran is applied2. 6. After the large hilling, herbicide is sprayed in time for soil sealing, 55 to 70 percent of metolachlor diuron 2700-2675L of weed stem leaves are added with water for directional spraying. Harvesting is carried out in late 12 months. 7. And (4) leveling and film covering the perennial root sugarcane by using a leveling machine in the middle ten days of the next 1 month. The field management in the later period is basically consistent with the new planted sugarcane. 8. In the mature period of the sugarcaneAnd (5) checking and accepting the sugarcane yield of the residential area, and simultaneously collecting soil and plant samples. The organic carbon content of the soil is measured by an oil bath heating potassium dichromate oxidation capacity measuring method, and the carbon content of the plants is measured by a TOC instrument. Collecting greenhouse gas samples by adopting a static box method, collecting greenhouse gas once a week after sugarcane is planted, continuously sampling for 7 days after fertilization or when rainfall is more than 20mm, and carrying out encrypted sampling and greenhouse gas determination chromatography. The sugarcane market price is calculated according to 520 Yuan.t, and the labor cost of the chemical fertilizer and pesticide mechanical tillage comprises the labor cost of land preparation, planting and ridging, a pesticide applying machine, fertilizer, pesticide and the middle part.|[0061] The conventional planting process comprises the following steps: the method comprises the steps of rotary tillage and soil preparation (the depth is about 17 cm) by a tractor, fertilizing, seed placing, soil covering and film covering by a planter, micro-planting by a small sugarcane banking machine in a seedling stage, fertilizing in an elongation stage and high banking (the banking height is 15-18 cm) by a large banking machine, chemical weeding and harvesting, leveling perennial sugarcane by a leveling machine in the next year, and finally ridge breaking, fertilizing and film covering (the later-stage field management is consistent with the new planted sugarcane).|[0062] Through the positioning monitoring of newly planted perennial roots for 2 years, compared with the habit of farmers, the sugarcane cultivation technical mode of the invention can increase the yield of sugarcane stalks by 16.13 t.hm in 2 years2The amplification is 15.67%; the labor cost of the mechanical tillage of the chemical fertilizer and the pesticide is reduced by 1538 yuan hm2(ii) a Increase of sugarcane yield value 9923 yuan hm2The net income is increased by 11461 yuan hm2(ii) a The biological carbon fixation amount of the sugarcane is increased by 274 t.hm2The amplification is 16.82 percent, the organic carbon of the soil is increased by 0.32 g/kg, and the soil CO is2And N2The cumulative total discharge amount of O is respectively reduced by 9.18 percent and 14.46 percent, and the cumulative total absorption amount of soil CH4 is increased by 29.56 percent; the lodging angle of the sugarcane is reduced by 87.90 percent. The technology reduces the production cost of the sugarcane, increases the yield of the sugarcane, improves the biological carbon fixation amount of the sugarcane and the organic matter content of soil, prevents the sugarcane from lodging, reduces the greenhouse gas emission of the soil of the sugarcane field, and has good economic benefit, ecological benefit and social benefit.|[0063] TABLE 1 analysis of sugarcane yield and ecological benefit under different cultivation|The above description is not intended to limit the present application, and the present application is not limited to the above examples, and those skilled in the art should understand that they can make various changes, modifications, additions or substitutions within the spirit and scope of the present application. (CN114680010)|TECHNICAL FIELD|[0001] The invention relates to the technical field of sugarcane planting, in particular to a high-yield planting method of sugar canes in a red soil area and with the functions of soil carbon sequestration and emission reduction.|BACKGROUND ART|[0002] Sugarcane, (academic name:Saccharumofficinarum) Saccharum officinarum, a large and solid herb growing for many years. The root is strong and developed. The height of the stalk is 3-6 m. The sugarcane is suitable for being planted in places with fertile soil, sufficient sunlight and large temperature difference in winter and summer. The sugarcane isThe most important sugar crops in China occupy a very important position in tropical regions. Sugarcane is perennial root crop, and can be harvested for 3-7 years after being managed in place and newly planted once. Newly planted sugarcane needs to be cultivated, sowed, intertillage weeding, fertilizing and hilling, harvested and other production links in sugarcane production, and perennial root sugarcane also needs to be cultivated, ploughed, weeding, fertilizing, hilling, harvested and other production links.|[0003] The traditional sugarcane planting mode is a man-and-animal-powered working mode, is low in efficiency and high in labor intensity, and has a great limiting effect on scale management of sugarcane production in China. With the increasing of labor cost in rural areas and the popularization of land circulation and mechanization, sugarcane planting develops towards the direction of mechanization planting, and people put forward a production idea of mechanization in the whole process of sugarcane production in recent years. However, due to factors such as drought in climate, degradation of variety, chemical fertilizer abuse, small scale and the like, especially mismatch between agricultural machinery and agricultural implements, mismatch between agricultural implements and agricultural implements, and mismatch between agricultural implements and agriculture, effective, ideal and seamless butt joint of whole-process mechanized operations of sugarcane planting production still cannot be realized, so that the labor cost of sugarcane planting rises dramatically, the income of sugarcane farmers is reduced sharply, the sugarcane planting area is reduced, the yield is reduced, and the supply of domestic sugarcane is seriously influenced.|[0004] Actual planting research finds that the current mechanical sugarcane planting management mode mainly has the following defects.|[0005] 1. In the traditional mechanized planting management process of the sugarcane, a large-scale tractor with high horsepower and high strength is mainly used for deep ploughing, rotary tillage, deep scarification and rotary tillage in the machine tillage and soil preparation process, and the defects that after the rotary tillage operation, the scarification depth is more than 25cm, the tillage layer is shallow, the sugarcane is shallow in root, the continuous utilization capability of water and fertilizer is poor, the sugarcane is easy to fall down, and the yield is low are caused. Although the ridge smashing machine is adopted for ridge smashing deep ploughing, the ploughing depth can reach 30-40 cm, the ridge smashing ploughing and deep ploughing plus rotary tillage, deep scarification plus rotary tillage are the same and need a tractor with larger horsepower to operate, the oil consumption is large, the energy saving and emission reduction are not facilitated, and the adopted ploughing mode is that the whole field soil is turned over generally, the soil disturbance is increased, so that the closed accumulation organic carbon protected by aggregates is rapidly utilized by microorganisms after being exposed, the organic carbon is mineralized, and the organic carbon is discharged and discarded in the form of carbon dioxide.|[0006] 2. In the aspect of mixing the sugarcane leaves and the soil, the deep ploughing operation can bury the sugarcane leaves into the subsoil, but the sugarcane leaves are decomposed in the subsoil layer, the nutrients of the sugarcane leaves are not easy to be absorbed and utilized by the sugarcane in the current year, and the deep ploughing operation mainly aims at the operation of directly ploughing and re-planting the sugarcane after crushing, but is not suitable for continuously lodging the root sugarcane plots. Because of the large amount of sugarcane leaves in the field, the rotary cultivator and the ridge smashing machine can not disperse the sugarcane leaves, so that the sugarcane leaves are piled up, soil is possibly lifted, the moisture in the soil is evaporated more quickly, the absorption of the sugarcane to moisture and nutrients is not facilitated, and the growth of sugarcane seedlings is influenced.|[0007] 3. The ridge-breaking ridging amount of the small ridging or perennial root sugarcane is large, soil extrudes the sugarcane to different degrees, tillering and stem forming rate of the sugarcane are influenced, and the group structure of the sugarcane is unreasonable; and the soil is sealed by adopting a herbicide after hilling, so that the labor and pesticide costs are increased.|[0008] 4. The intertillage large ridging mainly adopts a plough shovel type, spiral type or disc type intertillage ridging machine to carry out ditching ridging. The plow-shovel type banking machine has poor soil crushing capability; the spiral mechanical ridge shape has poor adaptability and large energy consumption, the soil throwing flow direction is not easy to control, the soil splashes at a high speed, and the injury of stems and leaves of crops and the personal safety are easy to cause; the disc type hiller is used for hilling sugarcane fields with hard soil, and the hilling depth and effect of the disc type hiller are inferior to those of a spiral type hiller. In general, the existing agricultural implements of the sugarcane intertillage hiller have poor fusion degree with agriculture, cause grinding, extrusion, pressing and covering to the sugarcane, and are difficult to meet the field operation.|[0009] 5. The perennial root sugarcane stumping mainly utilizes a stumping cutter head of a stumping machine to stump, and only can cut the sugarcane heads on the ground due to the horizontal rotation of the cutter head, so that the early germination of high-position buds is easily induced, the sugarcane seedlings are slender, and the germination of the low-position buds of the base parts is inhibited. And the output power of the tractor is unstable, which can cause the quality of stubble leveling of the sugarcane bags to be unstable and reduce the quality of perennial root sugarcane mulching films.|[0010] In order to better realize the mechanized production of the sugarcane, the high-yield sugarcane planting technology integrating the fine variety and fine method technical mode is designed, and the high-yield sugarcane planting technology is very necessary to be demonstrated and popularized in the Guangxi sugarcane planting area.|DISCLOSURE|Disclosure of Invention|[0011] The invention aims to provide a sugar cane high-yield planting method considering both carbon fixation and emission reduction of soil in a red soil area, which is a cultivation mode of 'interval local deep scarification and deep ploughing, uniform mixing of cane leaves and soil, deep planting, micro-cultivation for plant spacing, labor saving, fertilizer application and insect prevention for one time completion by using pesticide and fertilizer, high hilling and perennial root leveling and film covering', reduces the oil consumption of agricultural implement soil preparation and disturbance to soil, reduces organic carbon mineralization of soil, and reduces greenhouse gas emission; the problems that the conventional cultivated land is shallow in cultivation layer, large in intertillage and shallow in earthing up, and sugarcane falls down due to earthing up of a volcanic opening and the like are solved; the phenomenon that the straw piles influence the subsequent farming is reduced; labor cost for applying fertilizer and pesticide is reduced, and utilization rate of the fertilizer is improved; high hilling and perennial root flattening are combined, sugarcane is prevented from lodging, sugarcane bags are prevented from being rolled by a harvesting machine, high-position buds of perennial root sugarcane are prevented from early sprouting, the sugarcane yield is increased, and the perennial root sugarcane age is prolonged; finally achieving the purposes of carbon fixation and emission reduction of the soil of the sugarcane field, lodging resistance, and yield and efficiency increase of the sugarcane.|[0012] In order to realize the purpose of the invention, the technical scheme is as follows:|a high-yield planting method for sugar canes in a red soil area and with the functions of soil carbon sequestration and emission reduction is disclosed, which comprises the processes of sugarcane soil preparation, fertilization, seed arrangement, soil covering and film covering, ridging, weeding, harvesting, perennial root sugarcane leveling and film covering, and specifically comprises the following steps.|[0013] (1) Stubble cleaning and pre-ditching: and (3) crushing and stubble cleaning are carried out on the residues of the previous crops by adopting a stubble cleaning pre-furrowing machine, and meanwhile, linear pre-furrowing is carried out at a distance of 140cm, so as to linearly position the post-process.|[0014] (2) Local deep scarification and deep ploughing, ditching and base fertilizer application: adopting a tillage and soil preparation pipe all-in-one machine to carry out soil throwing type deep scarification and deep ploughing on broken soil in a ditch which is pre-opened, throwing the broken soil to two sides to form sugarcane planting ditches, wherein the width of each ditch is 70cm, two sides of each sugarcane planting ditch are not ploughed, and meanwhile, applying a special pesticide-fertilizer base fertilizer for sugarcane in the sugarcane planting ditches; the deep scarification, deep ploughing and soil breaking farming area occupies about one half of the original land, so that the oil consumption of agricultural implements and the disturbance to soil are reduced.|[0015] When the soil is crushed and thrown, the crushed soil and the broken straws of the previous stubbles are mixed uniformly, the problem that the straws are piled and erected in the empty soil when the common rotary cultivator works can be reduced, and the straw-stalk rotary cultivator can also be used for throwing the soilCan accelerate the decomposition of the straws and improve the organic matter content of the soil. The broken soil is thrown between the rows at two sides to form a concave groove with the planting depth being 20-25 cm lower than the original solid surface, the height from the bottom of the groove to the ridge surface being 50-60 cm, the width of the ridge surface being 50-60 cm and the width of the base of the ridge being 70cm, thus realizing deep planting of the sugarcane. For the lower part is real soil, the upper portion is for throwing the loose soil of going, and the maximum soaks the collection to concave type groove with natural precipitation like this, does benefit to soil and preserves water, and in the operation of ditching, the all-in-one is with fertilizer and the mixing of recess ditch soil, and fertilizer is only limited in recess ditch soil, realizes fertilizer deep fertilization, and recess ditch liquid manure coordinates, improves fertilizer utilization ratio, and sugarcane root system is perpendicular to prick anti lodging for the first time deeply. The base fertilizer is applied with the special pesticide fertilizer for the sugarcane, the fertilizer application and the pesticide application are carried out synchronously, the labor cost is reduced, and the application amount is N120 kg/hm2 、P2O5 80 kg/hm2 、K2O 150 kg/hm2The formula is suitable for the nutrient requirement of the sugarcane in the seedling stage, and the utilization rate of the fertilizer is improved. And the deep scarification, deep ploughing, ditching, soil throwing and fertilizing are completed by the all-in-one machine at one time, so that the labor efficiency is greatly improved.|[0016] (3) Seed arrangement, soil covering and film covering: carrying out automatic seed arrangement, soil covering and film covering planting by adopting a sugarcane planting machine, arranging two rows of sugarcane seeds in a sugarcane planting ditch, wherein the interval between the two rows of sugarcane seeds is 20 cm; the planter firstly loosens the soil on the two sides of the sugarcane seeds by unscrewing again to cover the soil on the sugarcane seeds. The covering soil for planting the sugarcane is thicker and about 9-11cm in autumn and winter, and is thinner and about 7-8cm in spring, so that early sprouting of the sugarcane seeds is facilitated. The degradable film with the width of 50 cm-60 cm is covered, when the film is pressed, the two sides of the mulching film are tightly pressed and tensioned, the film is not ventilated, the middle of the film is transparent for about 13-15cm, the water evaporation is prevented, the moisture is preserved, the temperature is kept, the sugarcane sprouts can be promoted only by water vapor below the ground without extra irrigation, the tensioned film is tightly attached to the ground, the sugarcane sprout top film breaking is facilitated, and the manual seedling picking operation cost is reduced. The sugarcane planter is purchased and used in the market or designed and used by the user.|[0017] (4) Fertilizing in seedling stage and physical weeding and micro-hilling: the sugarcane hiller is adopted, the seedling fertilizer N120 kg/hm2 is applied, the fertilizer is applied in combination, the sugarcane hiller carries out rotary tillage and soil throwing to turn the soil on the ridge surface to the ditch to cover 2-5 cm, micro-hilling is carried out, the phenomenon that large soil extrudes seedlings is avoided, the growing positions of the sugarcane seedlings can be scattered and positioned, the light transmittance and effective stems in the later period are increased, the moisture evaporation can be avoided, the sugarcane is promoted to root for the second time, row spacing weeds are rotated off in the rotary tillage and hilling process of the sugarcane hiller, and manual weeding and pesticide expenditure are reduced; the sugarcane banking machine is purchased or designed for use in the market.|[0018] (5) Fertilizing in the elongation period and high hilling: fertilizing and ridging operation is carried out by adopting the tillage and field management integrated machine in the step (2); applying sugarcane insecticide fertilizer, N260 kg/hm2、P2O5 40kg/hm2、K2O 150kg/hm2(ii) a The combined cutter rotating at high speed of the integrated tillage and soil preparation machine crushes soil on the ridge surface originally formed and then throws the crushed soil back to the base of the sugarcane plant, the ridging amount is 3 times of that of a conventional rotary cultivator, high ridging quality with full ridge shape, loose soil and complete and tight weed coverage is obtained, and the occurrence of 'fire hills' is reduced; after the hilling loose soil is solidified, the ridge height is 23-26cm, the sugarcane pocket is buried under the soil with the depth of 20-25 cm, the ridge surface width reaches 60-70 cm, and the ridge bottom width is 108-112cm, so that the lodging resistance of the sugarcane is improved, the crushing damage to the sugarcane pocket during mechanical harvesting is reduced, and the perennial root life is prolonged.|[0019] (6) Chemical weeding and harvesting: after the large hilling, the herbicide is sprayed in time for soil sealing, 55 to 70 percent of methyl, metolachlor, diuron 2700 and 3600g/hm2 are used for adding water 675L of weed stem leaves for directional spraying, or 200g/L of glufosinate ammonium 3000 and 4500 ml/hm2 Adding water 675L weed stem leaves, directionally spraying for 1 time, and preventing and treating for 12 times according to weed occurrence conditions at the later stage; the harvest can be carried out in the mature period of the sugarcane process.|[0020] (7) Leveling perennial root sugarcane and covering with a film: a ridge with the original height of 23-26cm of perennial root sugarcane is cut by a flattening machine with 13-16cm of sugarcane pocket, the ridge surface is smooth and convenient to cover with a film, soil on the ridge surface is thrown to the two outer sides of the sugarcane pocket, and the requirement of subsequent high hilling is met; after the ridge surface is leveled and reduced, the sugarcane is 10-12cm high in ridge, the perennial root sugarcane is covered with a film, water-retaining and heat-preserving, the germination of low-level buds is promoted, the emergence rate is improved, and the perennial root sugarcane age is prolonged; and (5) managing and harvesting according to the processes in the steps (4) to (6), wherein the perennial root sugarcanes adopt the processes until the sugarcane needs to be turned over again, and the sugarcane leaves are crushed and returned to the field after each batch of the sugarcane is harvested.|[0021] The integrated tillage and pipe-making machine is driven by a tractor in a traction way and comprises a rack and a gear box, wherein the gear box is arranged above the middle of the rack, power output shafts are respectively arranged at the left side and the right side of the gear box, and a power input main shaft which can be connected with a power shaft of the tractor is arranged at the front end of the gear box; the front end of the rack is provided with a side cantilever seat used for being connected with a side cantilever of a tractor in an installing way, and a middle cantilever seat used for being connected with a middle cantilever of the tractor in an installing way is arranged above the front end of the rack through a bracket; two sides of the lower part of the front end of the rack are respectively provided with a subsoiling plough through a subsoiling plough mounting seat, a gear transmission case is fixed on the rack right behind each subsoiling plough, the upper end of each gear transmission case is provided with a power input shaft, and the power input shaft is connected with a power output shaft through a coupling; two sides of the lower end of the gear transmission box are respectively provided with a driving shaft with the rotating direction opposite to the advancing direction of the integrated machine, and a plurality of rotary tillage soil throwing knives are arranged on the driving shaft through knife holders; a baffle is arranged at the lower part of the rack above the rotary tillage soil throwing cutter, one side of the baffle, which is far away from the gear transmission case, is hinged with a soil guide baffle through a hinge, the soil guide baffle is also connected with the rack through an angle adjusting rod, and the angle adjusting rod can adjust the opening angle of the soil guide baffle; the frame is provided with a fertilizing device which can automatically guide and convey fertilizer to the rear side of the gear transmission case.|[0022] Further preferably: fertilizing device include the fertilizer can, the fertilizer can passes through the fertilizer can rack-mount in the frame, install a motor gear case in the frame of fertilizer can lower part respectively, all be fixed with a lower fertile carousel that covers the fertilizer can play fertile mouthful in the pivot of motor gear case, the motor gear case utilizes the power drive of motor to descend fertile carousel rotatory, the outer wall of fertilizer can is provided with one and has the fertilizer scraping plate that is used for scraping the fertilizer in the fertile carousel down, scrape and install the lower fertile fill that is used for connecing the whereabouts fertilizer in the frame of fertilizer scraping plate below, the bottom intercommunication of lower fertile fill has the fertilizer guide pipe, the fertilizer guide pipe extends the rear side of gear drive case.|[0023] Further preferred is: the driving shaft is uniformly provided with three groups of rotary tillage soil throwing knives through the knife seats, each group of rotary tillage soil throwing knives consists of three rotary tillage soil throwing knives, and the three rotary tillage soil throwing knives are uniformly distributed on the knife seats, namely, are uniformly distributed on the circumference of the driving shaft.|[0024] Further preferred is: the rotary tillage soil throwing cutter comprises an L-shaped arc-shaped rotary tillage cutter and a soil throwing plate, a cutter handle is arranged at the straight end of the L-shaped arc-shaped rotary tillage cutter, a mounting hole for connecting and fixing the cutter handle with a cutter holder is formed in the cutter handle, the cutter handle is fixedly mounted with the cutter holder by adopting a bolt and a nut, and the soil throwing plate is fixed on the cambered surface of the uncut soil side of the arc-shaped end of the L-shaped arc-shaped rotary tillage cutter; the soil throwing plate and the knife face of the L-shaped arc rotary blade are arranged in an obtuse angle, and the angle of 120 plus 150 degrees is optimal. The soil throwing plate and the L-shaped arc rotary blade can also be integrally bent and formed.|[0025] Further preferred is: the deep scarification plough comprises a plough rod, a long tooth extending forwards is fixed on the front side of the bottom end of the plough rod, soil plowing plates inclining downwards from back to front are respectively arranged on the left side and the right side of the bottom end of the plough rod, and a short tooth extending forwards is fixed on the side, far away from the plough rod, of the front end of each soil plowing plate. Long tooth and short tooth correspond with the three groups of rotary tillage soil throwing knives of installation rear side, and long tooth and short tooth can be under the prerequisite that reduces the resistance as far as possible, plough the pine with earth, avoid the three groups of rotary tillage soil throwing knives of rear side can't realize local deep ploughing subsoiling hack.|[0026] Further preferred is: the left side and the right side of the plow lever above the soil plowing plate are respectively provided with a side plate which is opened backwards.|[0027] Further preferred is: the upper end of the plough rod is provided with a fixed mounting hole which is used for being fixedly connected with the deep scarification plough mounting seat.|[0028] The stubble cleaning pre-furrowing machine is driven by a tractor in a traction manner and comprises a machine frame I and a gear box I, wherein a side cantilever seat I used for being connected with a side cantilever of the tractor in an installation manner is arranged at the front end of the machine frame I, and a middle cantilever seat I used for being connected with a middle cantilever of the tractor in an installation manner is arranged above the front end of the machine frame I through a support I; the two sides of the front end of the machine frame I are respectively provided with a front scarification plough through scarification plough mounting seats, the distance between the two front scarification ploughs is determined according to the ditching planting row spacing, and the rear end machine frame I on the left side and the right side of each front scarification plough is respectively provided with a rear scarification plough through the scarification plough mounting seats; the rear end of the rack I is provided with a ditching plow frame, each ditching plow frame behind the front scarification plow is provided with a ditching and marking plow through a ditching plow mounting seat, the front scarification plow and the rear scarification plow carry out primary plow ditching, the farming resistance of the ditching and marking plow is reduced, the ditching and marking plow can plow deeper soil, and therefore the traction resistance of the whole combined machine is reduced; the gearbox I is arranged above the middle of the rack I, power output shafts I are respectively arranged on the left side and the right side of the gearbox I, and a power input main shaft I capable of being connected with a power shaft of a tractor is arranged at the front end of the gearbox I; the left side and the right side of the rack I are symmetrically and fixedly provided with a gear transmission case I, the upper end of the gear transmission case I is provided with a power input shaft I, and the power input shaft I is connected with a power output shaft I through a coupler I; a rotary tillage shaft is arranged between the lower ends of the two gear transmission boxes I through a bearing with a base, the rotary tillage shaft is connected with a gear in the gear transmission box I, and a stubble cleaning rotary blade is arranged on the rotary tillage shaft. According to production needs, the installation mode of the rear scarification plough, the ditching and scribing plough and the front scarification plough can be set to be in an up-and-down adjustable form, a plurality of adjusting holes can be formed in the plough rod, and the plurality of adjusting holes can be arranged to adjust the fixed positions of the plough rod seat and the plough rod so as to realize the height adjustment of the plough.|[0029] Further preferred is: the front end of the gear transmission case I is provided with a soil breaking plough, so that the gear transmission case I can cut into soil during tillage, and the stubble cleaning rotary blade can extend into the soil for tillage.|[0030] Further preferred is: frame I on install the baffle I that prevents earth and splash.|[0031] Further preferred is: the ditching plow frame is articulated to be installed in the rear end of frame I, the ditching plow frame still articulates with frame I or gear box I through hydraulic cylinder, hydraulic cylinder's jar seat is articulated with frame I or gear box I, hydraulic cylinder's piston rod is articulated with the ditching plow frame, through the upset of hydraulic cylinder control ditching plow frame, realize the control of the promotion of ditching marking plow and transferring.|[0032] The perennial root sugarcane is subjected to film covering, water retention and heat preservation, and a perennial root sugarcane root cutting, ridge breaking, fertilizing and film covering combined machine is adopted, is pulled by a tractor and comprises a rack III, wherein a side cantilever seat III used for being connected with a side cantilever of the tractor in an installing manner is arranged at the front end of the rack III, and a middle cantilever seat III used for being connected with a middle cantilever of the tractor in an installing manner is arranged above the front end of the rack III; a fertilizer box III is arranged on the rack III through a fertilizer box rack III, a gear box III driven by a hydraulic motor III is arranged on the rack III at the lower part of the fertilizer box III, and a lower fertilizer circular rotating disc III covering a fertilizer outlet at the bottom of the fertilizer box III is fixed on a rotating shaft of the gear box III; two sides of the outer wall of the fertilizer box III are respectively provided with a fertilizer scraping plate III for scraping the fertilizer in the lower fertilizer circular rotating disc III, two sides of the outer wall of the fertilizer box III are respectively provided with a lower fertilizer box III for receiving the falling fertilizer, and the bottom of the lower fertilizer box III is communicated with a fertilizer guide pipe III; two sides of the front end of the rack III are respectively provided with a root cutting and soil breaking rolling disc for cutting ridges and roots on two sides of a sugarcane ridge through rolling disc mounting seats, and the fertilizer guide pipe III extends to the rear outer side of the root cutting and soil breaking rolling disc; a film frame is arranged at the lower part of the rear end of the frame III, a film shaft for placing a mulching film is arranged on the film frame, and film pressing wheels for rolling two sides of the mulching film are arranged on the rear side of the film frame through wheel carriers; two sides of the rear end of the machine frame III are respectively provided with a hinge seat, two hinge seats are hinged with a mounting rod extending backwards, the bottom end of the mounting rod is connected with a tension spring connected with the bottom of the hinge seat, and the lower part of the rear end of the mounting rod is provided with a soil crushing and returning rolling disc used for scraping soil on two sides of a mulching film; the middle of the rear end of the rack III is connected with a support frame extending backwards, and two sides of the support frame are connected with mounting rods on two sides of the support frame through threaded adjusting connecting rods for limiting. The distance between the two soil crushing and returning rolling disks is larger than that between the two root cutting and soil breaking rolling disks, and the soil crushing and returning rolling disks crush soil and return to cover the two sides of the mulching film.|[0033] Further preferred is: the soil crushing and soil returning rolling disc comprises a rotating shaft seat and an installation rotating shaft, the installation rotating shaft is installed in the rotating shaft seat through a bearing, an arc-shaped soil returning circular disc is installed on the installation rotating shaft in a stretching mode, the top end of the rotating shaft seat is fixedly connected with a connecting shaft, a square shaft body and a threaded shaft body are arranged at the top end of the connecting shaft, and the threaded shaft body is located at the top of the square shaft body; the connecting axle passes through the axle sleeve to be connected with the installation pole, the vertical welded fastening of axle sleeve is at the end of installation pole, the upper end of axle sleeve is provided with the engaging lug, be provided with slot hole or a plurality of connecting hole on the engaging lug, the connecting axle passes and is equipped with the locking plate on the axle sleeve rear shape axle body, threaded shaft installs lock nut on one's body, be provided with the square hole that matches with square axle body on the locking plate, still be provided with the through-hole that corresponds with slot hole or connecting hole position on the engaging lug on the locking plate, the locking plate passes through the bolt and is connected with the engaging lug, through after unscrewing lock nut, the locking plate rotates, adjust the position of locking plate and engaging lug, realize the regulation of hack back soil rolling disc installation angle.|[0034] Further preferred is: the root cutting and soil breaking rolling disc comprises a root cutting rotating shaft and a rod seat, the root cutting rotating shaft is installed in the rod seat through a root cutting rotating shaft bearing, an arc root cutting disc is installed at the extending end of the root cutting rotating shaft, a rod seat installation plate used for being connected with the rolling disc installation seat through a bolt shaft is arranged at the top end of the arc root cutting disc through a connecting rod shaft, and the rod seat installation plate is located at the top of the connecting rod shaft. During installation, the arc-shaped surface of the arc-shaped root cutting disc is close to the perennial root sugarcane ridge, so that the problem that the sugarcane buds are broken due to the fact that soil is stirred towards the sugarcane when the arc-shaped root cutting disc cuts the root is avoided.|[0035] Further preferred is: the installation slot hole is formed in the rod seat installation plate, the installation position of the rolling disc installation seat is convenient to adjust due to the installation slot hole, and the installation angle of the root cutting and soil breaking rolling disc is achieved.|[0036] Further preferred is: arc hack dish's dish limit equipartition be provided with a plurality of soil cuts mouthful, the periphery is provided with a plurality of breachs promptly, can be better during the rotation smash earth and break ridge root cutting.|[0037] Further preferred is: the screw thread adjusting connecting rod comprises a connecting screw rod I, a screw rod connecting seat and a connecting screw rod II, the screw rod connecting seat is a hollow long connecting seat, the connecting screw rod I and the connecting screw rod II are respectively in threaded connection at two ends of the screw rod connecting seat, the connecting screw rod I is hinged to the mounting rod through a connecting lug ring, the connecting screw rod II is hinged to the supporting frame through the connecting lug ring, and a locking nut used for locking the connecting screw rod II and the screw rod connecting seat is installed on the connecting screw rod II.|[0038] Further preferred is: the middle part of lower fertile circle carousel III be provided with and avoid fertilizer to pile up the vertical circular cone housing at lower fertile circle carousel III middle part, the setting of circular cone housing will be followed the fertilizer that falls down in the fertilizer case III and led the periphery of delivering to fertile circle carousel III down.|[0039] Further preferred is: the conical housing is provided with a stirring blade for stirring fertilizer.|The sugar cane high-yield planting method considering both carbon fixation and emission reduction of the soil in the red soil area has the advantages that during the planting process, the local part of the sugar cane land is dug at intervals to reduce the soil disturbance, the disturbance of agricultural implements to the soil is reduced, and the greenhouse gas emission and the oil consumption of the agricultural implements are reduced; the sugarcane seeds are directly attached to the hard ground of the concave groove, and the method of promoting the germination of the sugarcane by using the ground gas is adopted; the soil crushing and throwing combined knife uniformly mixes the straws with soil, so that the problem that the stacking of the straws influences the subsequent farming is reduced, the decomposition of the straws is accelerated, and the organic matter content of the soil is improved; a planting method of deep planting of sugarcane, twice root-tying, high-cultivation lodging resistance, reduction of crater and prevention of rolling of a harvesting machine of a sugarcane pocket; a method for micro-hilling at the sugarcane seedling stage, fixing the growth position of the sugarcane seedlings, increasing the light transmittance and the number of effective stems at the later stage and physically weeding; the perennial root sugarcane is leveled and covered with a film, water retention and heat preservation are realized, the germination of low-position buds is promoted, the emergence rate is improved, and the age limit of the perennial root sugarcane is prolonged.|[0040] The planting method adopts the integrated machine of tillage, field preparation and management, which integrates the functions of deep tillage, deep scarification, ditching, soil breaking, fertilization, ridging and the like into a whole, has high working efficiency, and solves the problems that the traditional operation machine has single function and is not beneficial to the whole mechanized operation of sugarcane production; the rotary direction of the rotary tillage soil throwing cutter of the tillage and field management integrated machine is opposite to the advancing direction of the cultivator, the front part of the rotary tillage soil throwing cutter is provided with the deep scarification plough, the deep scarification plough and the deep scarification plough are matched to realize deep tillage and deep scarification, the key technology for realizing the difficult winding of weeds is realized, the continuous work of the cultivator is ensured, and the soil breaking and ridging operation is facilitated. And because the baffle and the soil guide baffle are arranged above the rotary tillage soil throwing knife, the broken soil thrown by the rotary tillage soil throwing knife can be guided to two sides by adjusting the opening angle of the soil guide baffle, the functions of ditching and earthing up can be realized, and the sugarcane buds cannot be extruded and damaged by throwing and earthing up, so that the earthing up effect is good. The fertilizer applying device guides the fertilizer to the rear side of the gear transmission box, and the rotary tillage soil throwing cutter rotates backwards to throw soil, so that the base fertilizer is positioned at the bottom of the sugarcane ditch, the base fertilizer drops to cover soil, the sugarcane seeds are separated from the base fertilizer, the phenomena of root burning and seed burning caused by fertilizer fermentation are avoided, and the germination rate and the survival rate of the sugarcane are improved. The subsoiling plough is provided with long teeth and short teeth which extend forwards, the long teeth and the short teeth correspond to three groups of rotary tillage soil throwing knives arranged on the rear side, the long teeth and the short teeth can loosen the soil plough on the premise of reducing resistance as much as possible, and the three groups of rotary tillage soil throwing knives on the rear side are favorable for realizing local subsoiling and soil crushing.|[0041] The stubble cleaning pre-ditching machine adopted by the planting method can complete stubble cleaning, local soil loosening and ditching at the same time, because the deep ditching planting can improve the drought resistance and lodging resistance of the sugarcane, and can also improve the yield of the sugarcane, but the one-time ditching planting of the tractor in the prior art can not meet the requirement, and the sugarcane field is reclaimed and reseeded, and the sugarcane field needs to be broken and returned to the field, stubble cleaning, soil loosening and ditching processes before reseeding and planting according to the agricultural production needs, the combined machine can loosen the soil, ditch and clear up the soil loosening, prepare for subsequent ditching and deep ditch planting, improve the walking route for the tractor, avoid the dragging of the deep ditching work by the subsequent tractor, improve the production efficiency and reduce the labor intensity; the front two sides of the front end of a frame I of the stubble ploughing pre-furrowing machine are respectively provided with a front scarification plough through a scarification plough mounting seat, the distance between the two front scarification ploughs is determined according to the row spacing of ditching planting, and the rear end frame I on the left side and the right side of each front scarification plough is respectively provided with a rear scarification plough through a scarification plough mounting seat; the rear end of the rack I is provided with a ditching plow frame, each ditching plow frame behind the front scarification plow is provided with a ditching and scribing plow through a ditching plow mounting seat, the matching mode of the front scarification plow and the two rear scarification plows is adopted for primary plowing and ditching, the farming resistance of the ditching and scribing plow is reduced, the ditching and scribing plow can plow deeper soil, and therefore the traction resistance of the whole combined machine is reduced; the front end of the gear transmission case I is provided with a soil breaking plough, so that the gear transmission case I can cut into soil during tillage, stubble cleaning rotary blades can extend into the soil for tillage, and thorough stubble cleaning is guaranteed.|[0042] The leveling machine adopted by the planting method can be used for downwards rotating and cutting the soil and the sugarcane heads of the upper stubble sugarcane ridges, the rotating and cutting depth is close to the height of the upper stubble sugarcane ridging, the limiting depth can be adjusted through the limiting wheel II, the soil leveling and cutting soil of the stubble cleaning rotary blade II is leveled by the soil leveling plough and is pushed towards sugarcane rows on two sides of the sugarcane ridges, so that enough soil is improved for the subsequent intertillage ridging, the growth of high-position buds is avoided, and the problem that the ratoon sugarcane ridging height is small because enough soil is not used for ridging during the intertillage ridging is avoided; the leveling machine can stir the crushed sugarcane leaves returned to the field and soil to return to the field, so that the sugarcane is decomposed into organic matters, and the sugarcane leaves returned to the field in the current year can provide nutrients for the growth of the sugarcane in the current year.|[0043] The perennial root sugarcane root cutting, ridge breaking, fertilizing and mulching combined machine adopted by the planting method can simultaneously cut roots, break ridges, fertilize and mulching on two sides of a perennial root sugarcane ridge, is high in working efficiency, and solves the problems of low germination rate, low tillering rate and low seedling rate of sugarcane high-position buds caused by the fact that a harvester and a conveyor are put into a field and rolled. The root cutting, ridge breaking, fertilization and film covering can be completed through one-time cultivation, fertilizers are accurately applied to the ridge sides of the sugarcanes, the mechanization degree of sugarcane planting management is improved, the yield per unit of the sugarcanes is improved, the perennial root age is prolonged, and the natural risk resistance is improved. The two sides of the front end of the frame III are respectively provided with a root cutting and soil breaking rolling disc through a root cutting and rolling disc mounting seat, the two root cutting and soil breaking rolling discs are used for cutting off lateral roots on two sides of a perennial root sugarcane ridge and turning over soil, the fertilizer guide pipe III applies fertilizer into the turned over soil, the arc-shaped surface of the arc root cutting disc is close to the perennial root sugarcane ridge, soil is turned over to the sugarcane when the arc root cutting disc is used for cutting the root, the sugarcane buds are pressed to be broken, and damage to soil loosening and fertilizing of the perennial root sugarcane can be reduced. Two sides of the rear end of the rack III are respectively provided with a hinge seat, two hinge seats are hinged with a mounting rod extending backwards, the bottom end of the mounting rod is connected with a tension spring connected with the bottom of the hinge seat, and the lower part of the rear end of the mounting rod is provided with a soil crushing and returning rolling disc used for scraping soil on two sides of a mulching film; the middle part of the rear end of the rack III is connected with a support frame extending backwards, and two sides of the support frame are respectively connected with mounting rods at two sides through a threaded adjusting connecting rod for limiting; the setting of structure like this can make the hack return soil rolling disc can paste tight ground all the time, can scrape the both sides of earth gland plastic film, guarantees that the plastic film both sides all have earth gland.|DRAWINGS DESCRIPTION|[0044] FIG. 1 is a schematic diagram of the structure of the integrated machine for tillage and soil preparation;|FIG. 2 is a schematic right-side view of FIG. 1;|FIG. 3 is a schematic structural view of a rotary tillage soil throwing blade;|FIG. 4 is a schematic top view of FIG. 3;|FIG. 5 is a schematic view of the construction of the subsoiler;|FIG. 6 is a schematic structural view of a stubble ploughing pre-furrowing machine adopted;|FIG. 7 is a schematic left side view of FIG. 6;|FIG. 8 is a top schematic view of FIG. 6;|FIG. 9 is a schematic structural view of a root-cutting, ridge-breaking, fertilizing and film-covering combined machine for perennial sugarcane;|FIG. 10 is a schematic left side view of FIG. 9;|FIG. 11 is a schematic top view of FIG. 9;|FIG. 12 is a schematic structural view of a root cutting and soil breaking rolling disc;|FIG. 13 is a schematic view taken from the direction A-A of FIG. 12;|FIG. 14 is a top schematic view of FIG. 12;|FIG. 15 is a schematic structural view of a soil crushing and returning rolling disc;|FIG. 16 is a schematic view of the mounting structure of the lower spheroidicity rotary table III;|FIG. 17 is a top schematic view of FIG. 16;|FIG. 18 is a schematic view of a threaded adjusting connecting rod;|the part names of the sequence numbers in the figure are:|1. a frame, 2, a fertilizer box frame, 3, a fertilizer guide pipe, 4, a fertilizer discharging bucket, 5, a motor gear box, 6, a fertilizer scraping plate, 7, a fertilizer discharging turntable, 8, a fertilizer box, 9, a middle cantilever seat, 10, a bracket, 11, a gear box, 12, a power input main shaft, 13, a power input shaft, 14, a gear transmission box, 15, a side cantilever seat, 16, a deep loosening plough mounting seat, 17, a deep loosening plough, 18, a rotary tillage soil throwing knife, 19, a knife seat, 20, a driving shaft, 21, a soil guide baffle, 22, a baffle, 23, a hinge, 24, an angle adjusting rod, 25, a power output shaft, 26, a coupler, 27, an L-shaped arc rotary tillage knife, 28, a soil throwing plate, 29, a knife handle, 30, a mounting hole, 31, a short tooth, 32, a soil throwing plate, 33, a side plate, 34, a plough rod, 35, a fixed mounting hole, 36, a long tooth, 37, a broken soil, 38, a gear transmission box I, 39 and a bearing with a seat, 40. rotary tillage shaft, 41, stubble ploughing rotary blade, 42, machine frame I, 43, baffle I, 44, power input shaft I, 45, coupling I, 46, side cantilever base I, 47, power output shaft I, 48, gear box I, 49, power input main shaft I, 50, middle cantilever base I, 51, support I, 52, rear scarification plough, 53, ditching and marking plough, 54, front scarification plough, 55, scarification plough mounting base, 56, ditching mounting base, 57, ditching plough frame, 58, hydraulic cylinder, 59, root cutting and breaking rolling disc, 60, side cantilever base III, 61, machine frame III, 62, rolling disc mounting base, 63, hydraulic motor III, 64, gear box III, 65, middle cantilever base III, 66, fertilizer box frame III, 67, fertilizer box III, 68, fertilizer scraping plate III, 69, fertilizer circular fertilizer rotating disc, 70, fertilizer bucket, 71, hinged base, 72, tension spring, 73, threaded connecting rod, 74. the soil back-grinding device comprises a support frame, 75, an installation rod, 76, a locking plate, 77, a soil back-grinding rolling disc, 78, a film pressing wheel, 79, a wheel frame, 80, a film shaft, 81, a film frame, 82, a fertilizer guide pipe III, 83, a conical housing, 84, a toggle blade, 85, a root cutting rotating shaft, 86, a root cutting rotating shaft bearing, 87, a rod seat, 88, a rod seat installation plate, 89, an installation long hole, 90, an arc root cutting disc, 91, a soil cutting opening, 92, a rotating shaft seat, 93, a connecting shaft, 94, a square shaft body, 95, a threaded shaft body, 96, an arc soil back-grinding disc, 97, an installation rotating shaft, 98, a connecting screw rod I, 99, a screw rod connection seat, 100, a locking nut, 101 and a connecting screw rod II.|INVENTION MODE|Detailed Description|[0045] The present application will be described in further detail with reference to the accompanying drawings and examples.|[0046] Example 1|The sugar cane high-yield planting method can realize the high-yield planting of the sugar cane in the red soil area with the functions of carbon sequestration and emission reduction of the soil by adopting the following steps:|(1) stubble cleaning and pre-ditching: and (3) crushing and stubble cleaning are carried out on the residues of the previous crops by adopting a stubble cleaning pre-furrowing machine, and meanwhile, linear pre-furrowing is carried out at a distance of 140cm, so as to linearly position the post-process.|[0047] (2) Local deep scarification and deep ploughing, ditching and base fertilizer application: adopting a tillage and soil preparation pipe all-in-one machine to carry out soil throwing type deep scarification and deep ploughing on broken soil in a ditch which is pre-opened, throwing the broken soil to two sides to form sugarcane planting ditches, wherein the width of each ditch is 70cm, two sides of each sugarcane planting ditch are not ploughed, and meanwhile, applying a special pesticide-fertilizer base fertilizer for sugarcane in the sugarcane planting ditches; the deep scarification, deep ploughing and soil breaking farming area occupies about one half of the original land, so that the oil consumption of agricultural implements and the disturbance to soil are reduced.|[0048] When the soil is crushed and thrown, the crushed soil and the broken straws of the previous stubbles are uniformly mixed, so that the problem of the straw pile-up and empty soil during the operation of the common rotary cultivator can be solved, the decomposition of the straws can be accelerated, and the organic matter content of the soil can be improved. The broken soil is thrown between the rows at two sides to form a concave groove with the planting depth being 20-25 cm lower than the original solid surface, the height from the bottom of the groove to the ridge surface being 50-60 cm, the width of the ridge surface being 50-60 cm and the width of the base of the ridge being 70cm, thus realizing deep planting of the sugarcane. For the lower part is real soil, the upper portion is for throwing the loose soil of going, and the maximum soaks the collection to concave type groove with natural precipitation like this, does benefit to soil and preserves water, and in the operation of ditching, the all-in-one is with fertilizer and the mixing of recess ditch soil, and fertilizer is only limited in recess ditch soil, realizes fertilizer deep fertilization, and recess ditch liquid manure coordinates, improves fertilizer utilization ratio, and sugarcane root system is perpendicular to prick anti lodging for the first time deeply. The base fertilizer is applied with the special pesticide fertilizer for the sugarcane, the fertilizer application and the pesticide application are carried out synchronously, the labor cost is reduced, and the application amount is N120 kg/hm2 、P2O5 80 kg/hm2 、K2O 150 kg/hm2The formula is suitable for the nutrient requirement of the sugarcane in the seedling stage, and the utilization rate of the fertilizer is improved. And the deep scarification, deep ploughing, ditching, soil throwing and fertilizing are completed by the all-in-one machine at one time, so that the labor efficiency is greatly improved.|[0049] (3) Seed arrangement, soil covering and film covering: carrying out automatic seed arrangement, soil covering and film covering planting by adopting a sugarcane planting machine, arranging two rows of sugarcane seeds in a sugarcane planting ditch, wherein the interval between the two rows of sugarcane seeds is 20 cm; the planter firstly loosens the soil on the two sides of the sugarcane seeds by unscrewing again to cover the soil on the sugarcane seeds. The covering soil for planting the sugarcane is thicker and about 9-11cm in autumn and winter, and is thinner and about 7-8cm in spring, so that early sprouting of the sugarcane seeds is facilitated. The degradable film with the width of 50 cm-60 cm is covered, when the film is pressed, the two sides of the mulching film are tightly pressed and tensioned, the film is not ventilated, the middle of the film is transparent for about 13-15cm, the water evaporation is prevented, the moisture is preserved, the temperature is kept, the sugarcane sprouts can be promoted only by water vapor below the ground without extra irrigation, the tensioned film is tightly attached to the ground, the sugarcane sprout top film breaking is facilitated, and the manual seedling picking operation cost is reduced. The sugarcane planter is purchased and used in the market or designed and used by the user.|[0050] (4) Fertilizing in seedling stage and physical weeding and micro-hilling: the sugarcane hiller is adopted, the seedling fertilizer N120 kg/hm2 is applied, the fertilizer is applied in combination, the sugarcane hiller carries out rotary tillage and soil throwing to turn the soil on the ridge surface to the ditch to cover 2-5 cm, micro-hilling is carried out, the phenomenon that large soil extrudes seedlings is avoided, the growing positions of the sugarcane seedlings can be scattered and positioned, the light transmittance and effective stems in the later period are increased, the moisture evaporation can be avoided, the sugarcane is promoted to root for the second time, row spacing weeds are rotated off in the rotary tillage and hilling process of the sugarcane hiller, and manual weeding and pesticide expenditure are reduced; the sugarcane banking machine is purchased or designed for use in the market.|[0051] (5) Fertilizing in the elongation period and high hilling: fertilizing and ridging operation is carried out by adopting the tillage and field management integrated machine in the step (2); applying sugarcane insecticide fertilizer, N260 kg/hm2、P2O5 40kg/hm2、K2O 150kg/hm2(ii) a The combined cutter rotating at high speed of the integrated tillage and soil preparation machine crushes soil on the ridge surface originally formed and then throws the crushed soil back to the base of the sugarcane plant, the ridging amount is 3 times of that of a conventional rotary cultivator, high ridging quality with full ridge shape, loose soil and complete and tight weed coverage is obtained, and the occurrence of 'fire hills' is reduced; after the hilling loose soil is solidified, the ridge height is 23-26cm, the sugarcane pocket is buried under the soil with the depth of 20-25 cm, the ridge surface width reaches 60-70 cm, and the ridge bottom width is 108-112cm, so that the lodging resistance of the sugarcane is improved, the crushing damage to the sugarcane pocket during mechanical harvesting is reduced, and the perennial root life is prolonged.|[0052] (6) Chemical weeding and harvesting: after the large hilling, the herbicide is sprayed in time for soil sealing, 55 to 70 percent of methyl, metolachlor, diuron 2700 and 3600g/hm2 are used for adding water 675L of weed stem leaves for directional spraying, or 200g/L of glufosinate ammonium 3000 and 4500 ml/hm2 Adding water 675L weed stem leaves, directionally spraying for 1 time, and preventing and treating for 12 times according to weed occurrence conditions at the later stage; the harvest can be carried out in the mature period of the sugarcane process.|[0053] (7) Leveling perennial root sugarcane and covering with a film: a ridge with the original height of 23-26cm of perennial root sugarcane is cut by a flattening machine with 13-16cm of sugarcane pocket, the ridge surface is smooth and convenient to cover with a film, soil on the ridge surface is thrown to the two outer sides of the sugarcane pocket, and the requirement of subsequent high hilling is met; after the ridge surface is leveled and reduced, the sugarcane is 10-12cm high in ridge, the perennial root sugarcane is covered with a film, water-retaining and heat-preserving, the germination of low-level buds is promoted, the emergence rate is improved, and the perennial root sugarcane age is prolonged; and (5) managing and harvesting according to the processes in the steps (4) to (6), wherein the perennial root sugarcanes adopt the processes until the sugarcane needs to be turned over again, and the sugarcane leaves are crushed and returned to the field after each batch of the sugarcane is harvested.|[0054] The integrated tillage and pipe-making machine is driven by a tractor in a traction way and comprises a rack 1 and a gear box 11, wherein the gear box 11 is arranged above the middle of the rack 1, the left side and the right side of the gear box 11 are respectively provided with a power output shaft 25, and the front end of the gear box 11 is provided with a power input main shaft 12 which can be connected with the power shaft of the tractor; a side cantilever seat 15 used for being connected with a side cantilever of a tractor in an installing way is arranged at the front end of the frame 1, and a middle cantilever seat 9 used for being connected with a middle cantilever of the tractor in an installing way is arranged above the front end of the frame 1 through a support 10; the deep loosening plough 17 is mounted on two sides of the lower portion of the front end of the frame 1 through deep loosening plough mounting seats 16 respectively, the deep loosening plough 17 comprises a plough rod 34, a long tooth 36 extending forwards is fixed on the front side of the bottom end of the plough rod 34, soil plowing plates 32 inclining downwards from back to front are arranged on the left side and the right side of the bottom end of the plough rod 34 respectively, and a short tooth 31 extending forwards is fixed on the side, far away from the plough rod 34, of the front ends of the soil plowing plates 32. The left side and the right side of a plow rod 34 above the soil plowing plate 32 are respectively provided with a side plate 33 which is opened backwards. The upper end of the plow lever 34 is provided with a fixed mounting hole 35 for connecting and fixing with the deep loosening plow mounting base 16. A gear transmission case 14 is fixed on the frame 1 right behind each subsoiling plough 17, a power input shaft 13 is mounted at the upper end of the gear transmission case 14, and the power input shaft 13 is connected with a power output shaft 25 through a coupling 26; two sides of the lower end of the gear transmission box 14 are respectively provided with a driving shaft 20 with the rotation direction opposite to the advancing direction of the all-in-one machine, three groups of rotary tillage soil throwing knives 18 are uniformly distributed on each driving shaft 20 through a knife seat 19, and the three groups of rotary tillage soil throwing knives 18 respectively correspond to one knife seat 19; each group of rotary tillage soil throwing blades 18 consists of three rotary tillage soil throwing blades 18, and the three rotary tillage soil throwing blades 18 are uniformly distributed on a blade holder 19, namely on the circumference of a driving shaft 20. The rotary tillage soil throwing blade 18 comprises an L-shaped arc rotary tillage blade 27 and a soil throwing plate 28, a knife handle 29 is arranged at the straight end of the L-shaped arc rotary tillage blade 27, a mounting hole 30 for connecting and fixing the knife handle 29 with the knife holder 19 is formed in the knife handle 29, and the soil throwing plate 28 is fixed on the arc surface of the non-soil cutting side of the arc end of the L-shaped arc rotary tillage blade 27; the soil throwing plate 28 and the blade face of the L-shaped arc rotary blade 27 are arranged in an obtuse angle. The soil throwing plate 28 and the L-shaped arc rotary blade 27 can also be integrally formed by bending. A baffle 22 is arranged at the lower part of the frame 1 above the rotary tillage soil throwing knife 18, one side of the baffle 22 far away from the gear transmission case 14 is hinged with a soil guiding baffle 21 through a hinge 23, the soil guiding baffle 21 is also connected with the frame 1 through an angle adjusting rod 24, and the angle adjusting rod 24 can adjust the opening angle of the soil guiding baffle 21; a fertilizing device which can automatically guide fertilizer to the rear side of the gear transmission case 14 is arranged on the frame 1; fertilizer injection unit include fertilizer box 8, fertilizer box 8 passes through fertilizer box frame 2 and installs in frame 1, install a motor gear box 5 on the frame 1 of 8 lower parts of fertilizer box respectively, all be fixed with a lower fertilizer carousel 7 that covers 8 fertilizer outlets of fertilizer box in the pivot of motor gear box 5, motor gear box 5 utilizes the power drive of motor to descend fertilizer carousel 7 rotatory, fertilizer box 8's outer wall is provided with one and is used for scraping the fertilizer in lower fertilizer carousel 7 and scrapes fertilizer board 6, scrape and install the lower fertilizer fill 4 that is used for connecing the whereabouts fertilizer on the frame 1 of fertilizer board 6 below, the bottom intercommunication of lower fertilizer fill 4 has fertilizer guide 3, fertilizer guide 3 extends gear drive case 14 rear side.|[0055] The working principle of the adopted tillage and soil preparation pipe all-in-one machine is as follows: the side cantilever and the side cantilever seat 15 of the tractor are connected in an installing way, the middle cantilever and the middle cantilever seat 9 of the tractor are connected in an installing way, and the side cantilever and the middle cantilever of the tractor are used for controlling the lifting and lowering of the tillage and soil preparation pipe all-in-one machine. When the cultivator is not used for cultivating, the cultivator-pipe integrated machine is lifted by the side cantilever and the middle cantilever of the tractor. When the sugarcane is planted, the tractor puts the tillage and soil preparation pipe all-in-one machine down, fertilizer is put into the fertilizer box 8, the tractor is driven to travel by traction, the motor gear box 5 drives the fertilizer-discharging rotary disc 7 to rotate by the power of the motor, and the deep scarification plough 17 cuts and digs soil, so that the working resistance of the rotary tillage soil-throwing knife 18 arranged at the rear side can be reduced, and the local deep tillage and deep scarification of the rotary tillage soil-throwing knife 18 are facilitated; the power output by the tractor is transmitted into the gear box 11 from the power input main shaft 12, the power is respectively transmitted to the power input shaft 13 from the power output shafts 25 at two sides of the gear box 11 through the shaft couplings 26, the power is transmitted into the gear transmission box 14, the driving shaft 20 is driven to drive the rotary tillage soil throwing cutter 18 to rotate backwards to break soil and throw soil through the action of the soil guide baffle plate 21 and the baffle plate 22, soil is turned and thrown towards two sides to form a sugarcane planting ditch, the fertilizer in the fertilizer box 8 falls onto the lower fertilizer rotating disc 7, the fertilizer in the lower fertilizer rotating disc 7 is scraped into the lower fertilizer bucket 4 due to the rotation of the lower fertilizer rotating disc 7 and the blocking action of the fertilizer scraping plate 6, the fertilizer is discharged into the sugarcane planting ditch through the action of the fertilizer guide pipe 3, a small part of broken soil falls into the ditch during the working process of the rotary tillage soil throwing cutter to cover the fertilizer, and the fertilizer is separated from the sugarcane when the sugarcane seeds fall into the ditch, avoids the phenomena of root burning and seed burning caused by fertilizer fermentation, and improves the germination rate and the survival rate of the sugarcane. When the soil is required to be hilled, the fertilizer applying device is stopped to work, and the opening angle of the soil guide baffle 21 is adjusted to enable soil to be turned over towards the root of the sugarcane ridge.|[0056] The stubble-cleaning pre-furrowing machine is driven by a tractor in a traction manner and comprises a machine frame I42 and a gear box I48, wherein a side cantilever seat I46 used for being connected with a side cantilever of the tractor in an installation manner is arranged at the front end of the machine frame I42, and a middle cantilever seat I50 used for being connected with a middle cantilever of the tractor in an installation manner is arranged above the front end of the machine frame I42 through a support I51; the two sides of the front end of the frame I42 are respectively provided with a front scarification plough 54 through a scarification plough mounting seat 55, the distance between the two front scarification ploughs 54 is determined according to the row spacing of ditching and planting, and the rear end frame I42 at the left side and the right side of each front scarification plough 54 is respectively provided with a rear scarification plough 52 through the scarification plough mounting seat 55; the ditching plow frame 57 is hinged to the rear end of the machine frame I42, a ditching and marking plow 53 is mounted on the ditching plow frame 57 behind each front scarification plow 54 through a ditching plow mounting seat 56, the front scarification plow 54 and the rear scarification plow 52 carry out primary plow ditching, the farming resistance of the ditching and marking plow 53 is reduced, the ditching and marking plow 53 can plow deeper soil, and the traction resistance of the whole combined machine is reduced; the ditching plow frame 57 is also hinged with the machine frame I42 or the gear box I48 through a hydraulic oil cylinder 58, a cylinder seat of the hydraulic oil cylinder 58 is hinged with the machine frame I42 or the gear box I48, a piston rod of the hydraulic oil cylinder 58 is hinged with the ditching plow frame 57, the ditching plow frame 57 is controlled to turn through the hydraulic oil cylinder 58, and the control of lifting and lowering of the ditching marking plow 53 is realized. A baffle I43 for preventing mud from splashing is mounted on the machine frame I42. The gearbox I48 is arranged above the middle of the rack I42, power output shafts I47 are respectively arranged on the left side and the right side of the gearbox I48, and a power input main shaft I49 capable of being connected with a power shaft of a tractor is arranged at the front end of the gearbox I48; the left side and the right side of the rack I42 are symmetrically and fixedly provided with a gear transmission box I38, the upper end of the gear transmission box I38 is provided with a power input shaft I44, and the power input shaft I44 is connected with a power output shaft I47 through a coupler I45; a rotary tillage shaft 40 is arranged between the lower ends of the two gear transmission boxes I38 through a bearing 39 with a base, the rotary tillage shaft 40 is connected with a gear in the gear transmission box I38, and a stubble cleaning rotary blade 41 is arranged on the rotary tillage shaft 40. The front end of the gear transmission box I38 is provided with a soil breaking plough 37, so that the gear transmission box I38 can cut into soil during tillage, and the stubble cleaning rotary blade 41 can extend into the soil for tillage.|[0057] The working principle of the stubble-cleaning pre-furrowing machine is as follows: the side cantilever of a tractor is connected with a side cantilever seat I46 in an installing way, the middle cantilever of the tractor is connected with a middle cantilever seat I50 in an installing way, a power shaft at the rear end of the tractor is connected with a power input main shaft I49, and the tractor controls the combination machine to ascend and descend; hydraulic rams 58 are connected to a hydraulic cylinder control system. When the combined machine is not used for tillage during walking, the combined machine is lifted through the side cantilever and the middle cantilever of the tractor, and the ditching plow frame 57 is turned upwards by the hydraulic oil cylinder 58. When the land needs to be cultivated, the tractor lowers the combined machine and drives the combined machine to walk, the power output by the tractor is transmitted into the gear box I48 from the power input main shaft I49, the power is respectively transmitted to the power input shaft I44 from the power output shafts I47 at the two sides of the gear box I48 through the shaft coupling I45, the power is transmitted into the gear transmission box I38 of the frame I42, the rotary tillage shaft 40 is driven to drive the stubble-cleaning rotary blade 41 to rotate and clean the stubble after being transmitted by the gears in the gear transmission box I38, the soil breaking plough 37 at the front end of the gear transmission box I38 breaks the soil, the gear transmission case I38 is enabled to cut into soil, the front scarification plough 54 and the rear scarification plough 52 carry out primary plough ditching, the farming resistance of the ditching and marking plough 53 is reduced, the hydraulic oil cylinder 58 turns the ditching plough frame 57 downwards, the ditching and marking plough 53 ploughs into the soil, ditching and soil loosening are cleaned, preparation is made for subsequent ditching and deep groove planting, the walking route is also improved for the tractor, and the tractor is prevented from working and slipping. The pre-ditching can pull loose soil open, when the following tractor pulls the deep ditching, the tractor runs and skids, if the pre-ditching is not carried out, when the tractor pulls the deep ditching, the tractor wheel is easy to skid, and the deep ditching can be realized very much.|[0058] The perennial root sugarcane is subjected to film covering, water retention and heat preservation, and a perennial root sugarcane root cutting, ridge breaking, fertilizing and film covering combined machine is adopted and comprises a rack III 89, the front end of the rack III 89 is provided with a side cantilever seat III 88 for being connected with a side cantilever of a tractor in an installing manner, and a middle cantilever seat III 93 for being connected with a middle cantilever of the tractor in an installing manner is arranged above the front end of the rack III 89; a fertilizer box III 95 is arranged on the rack III 89 through a fertilizer box rack III 94, a gear box III 92 driven by a hydraulic motor III 91 is arranged on the rack III 89 at the lower part of the fertilizer box III 95, and a lower fertilizer circular rotating disc III 97 covering a fertilizer outlet at the bottom of the fertilizer box III 95 is fixed on a rotating shaft of the gear box III 92; two sides of the outer wall of the fertilizer box III 95 are respectively provided with a fertilizer scraping plate III 96 used for scraping the fertilizer in the lower fertilizer circular turntable III 97, two sides of the outer wall of the fertilizer box III 95 are respectively provided with a lower fertilizer bucket III 98 used for receiving the falling fertilizer, and the bottom of the lower fertilizer bucket III 98 is communicated with a fertilizer guide pipe III 110; two sides of the front end of the rack III 89 are respectively provided with a root cutting and soil breaking rolling disc 87 for breaking ridges and cutting roots on two sides of a sugarcane ridge through rolling disc mounting seats 90, and the fertilizer guide pipe III 110 extends to the rear outer side of the root cutting and soil breaking rolling disc 87; a film frame 109 is arranged at the lower part of the rear end of the rack III 89, a film shaft 108 for placing a mulching film is arranged on the film frame 109, and a film pressing wheel 106 for rolling the two sides of the mulching film is arranged at the rear side of the film frame 109 through a wheel carrier 107; two sides of the rear end of the rack III 89 are respectively provided with a hinge seat 99, two hinge seats 99 are hinged with a mounting rod 103 extending backwards, the bottom end of the mounting rod 103 is connected with a tension spring 100 connected with the bottom of the hinge seat 99, and the lower part of the rear end of the mounting rod 103 is provided with a soil crushing and returning rolling disc 105 used for scraping soil on two sides of a mulching film; the middle part of the rear end of the rack III 89 is connected with a support frame 102 extending backwards, and two sides of the support frame 102 are respectively connected with mounting rods 103 at two sides through a threaded adjusting connecting rod 101 for limiting. The distance between the two soil breaking and returning rolling disks 105 is larger than the distance between the two root cutting and soil breaking rolling disks 87. The soil crushing and soil returning rolling disc 105 comprises a rotating shaft seat 120 and an installation rotating shaft 125, the installation rotating shaft 125 is installed in the rotating shaft seat 120 through a bearing, an arc-shaped soil returning circular disc 124 is installed on the installation rotating shaft 125 in a stretching mode, the top end of the rotating shaft seat 120 is fixedly connected with a connecting shaft 121, a square shaft body 122 and a threaded shaft body 123 are arranged at the top end of the connecting shaft 121, and the threaded shaft body 123 is located at the top of the square shaft body 122; connecting axle 121 passes through the axle sleeve and is connected with installation pole 103, the vertical welded fastening of axle sleeve is at the end of installation pole 103, the upper end of axle sleeve is provided with the engaging lug, be provided with slot hole or a plurality of connecting hole on the engaging lug, connecting axle 121 is equipped with locking plate 104 on passing square axle body 122 behind the axle sleeve, install lock nut on the screw thread axle body 123, be provided with the square hole that matches with square axle body 122 on the locking plate 104, still be provided with the through-hole that corresponds with slot hole or connecting hole position on the engaging lug on the locking plate 104, locking plate 104 passes through the bolt and is connected with the engaging lug, through unscrewing the lock nut after, lock plate 104 rotates, adjust the position of locking plate 104 and engaging lug, realize the regulation of hack return native rolling disc 105 installation angle. The root cutting and soil breaking rolling disc 87 comprises a root cutting rotating shaft 113 and a rod seat 115, the root cutting rotating shaft 113 is installed in the rod seat 115 through a root cutting rotating shaft bearing 114, an arc-shaped root cutting disc 118 is installed at the extending end of the root cutting rotating shaft 113, the top end of the arc-shaped root cutting disc 118 is provided with a rod seat installation plate 116 which is connected with the rolling disc installation seat 90 through bolts through a connecting rod shaft, and the rod seat installation plate 116 is located at the top of the connecting rod shaft. The rod seat mounting plate 116 is provided with a mounting long hole 117, the mounting position of the rolling disc mounting seat 90 can be conveniently adjusted by the mounting long hole 117, and the mounting angle of the root cutting and soil breaking rolling disc 87 is realized. The plate edge of the arc soil crushing plate 23 is uniformly provided with a plurality of soil cutting openings 119. The thread adjusting connecting rod 101 comprises a connecting screw I126, a screw connecting seat 127 and a connecting screw II 129, the screw connecting seat 127 is a hollow long connecting seat, the connecting screw I126 and the connecting screw II 129 are respectively in threaded connection with two ends of the screw connecting seat 127, the connecting screw I126 is hinged to the mounting rod 103 through a connecting lug ring, the connecting screw II 129 is hinged to the supporting frame 102 through the connecting lug ring, and a locking nut 128 used for locking the connecting screw II 129 and the screw connecting seat 127 is mounted on the connecting screw II 129. The middle part of lower fertile circle carousel III 97 be provided with and avoid fertilizer to pile up the vertical circular cone housing 111 in lower fertile circle carousel III 97 middle part, the setting of circular cone housing 111 will be from the fertilizer that falls in the fertile case III 95 lead the periphery of delivering to fertile circle carousel III 97 down. The conical housing 111 is provided with a stirring blade 112 for stirring fertilizer.|[0059] The operating principle of the perennial sugarcane root cutting, ridge breaking, fertilizing and film covering combined machine is as follows: the side cantilever and the side cantilever seat III 88 of the tractor are connected in an installing mode, the middle cantilever and the middle cantilever seat III 93 of the tractor are connected in an installing mode, and the side cantilever and the middle cantilever of the tractor are used for controlling the rising and the lowering of the perennial sugarcane root cutting, ridge breaking, fertilizing and mulching combined machine. According to the actual ridge width of the perennial root sugarcane, the distance between the two root cutting and soil breaking rolling discs 87 is adjusted by adjusting the installation positions of the rolling disc installation seats 90, and the distance between the two installation rods 103 is adjusted by adjusting the installation positions of the hinged seats 99, so that the distance between the soil breaking and soil returning rolling discs 105 is adjusted;|when the sugarcane harvester is not used for farming during walking, the perennial sugarcane root cutting, ridge breaking, fertilizing and mulching combined machine is lifted through the side cantilever and the middle cantilever of the tractor. When the land needs to be cultivated, a tractor lowers a ratoon sugarcane root cutting, ridge breaking, fertilizing and mulching combined machine, two root cutting, soil breaking and rolling disks 87 are positioned on two sides of a sugarcane ridge, fertilizer is put into a fertilizer box III 95, a mulching film roll is collided on a film shaft 108, a film pressing wheel 106 is favorable for pressing two sides of a mulching film, the tractor drives the sugarcane to travel, meanwhile, a hydraulic motor III 91 drives a lower fertilizer circle rotating disk III 97 to rotate through a gear box III 92, and the two root cutting, soil breaking and rolling disks 87 cut off and turn over soil on the side roots on the two sides of the ratoon sugarcane ridge; the fertilizer in the fertilizer box III 95 falls on the lower fertilizer circular turntable III 97, the fertilizer in the lower fertilizer circular turntable III 97 is scraped to fall into the lower fertilizer bucket III 98 due to the rotation of the lower fertilizer circular turntable III 97 and the blocking action of the fertilizer scraping plate III 96, the fertilizer is discharged to the lower part of soil stirred by the root cutting and soil breaking rolling disc 87 under the action of the fertilizer guide pipe III 110, the soil breaking and soil returning rolling disc 105 is dragged at the rear side to cut and break the soil, the mulching is finished by guiding the two sides of the mulching film to be covered, the root cutting and ridge breaking, the fertilization and the mulching of the perennial sugarcane can be finished by one-time operation, and the sprouting and the growth of the perennial sugarcane are facilitated.|[0060] Application case|The high-yield planting method for sugar cane carries out test demonstration in the town of Wuming Altar at 2020, 1 month to 2021, 12 months, designs two treatments of conventional cultivation of farmers and cultivation of the invention, and each treated land is 666.6m2This was repeated three times. The high-yield planting method of the sugar cane comprises the following specific steps:|1. in 1 month, 120 horsepower rotary cultivator equipped with Beidou navigation system is adopted, the residue of the previous crop is crushed and stubble-cleaned, and meanwhile, the straight line with the distance of 140cm is pre-ditched. 2. Adopting a deep scarification and deep ploughing, soil crushing, soil throwing, ditching and fertilizing all-in-one machine, locally and deeply ploughing, soil crushing and throwing and ditching, throwing soil into the space between two side rows to form a planting ditch with the depth being 20 cm-25 cm lower than the original field surface, forming a concave groove below the ground solid soil, the height from the ditch bottom to the ridge surface being 50 cm-60 cm, the width of the ridge surface being 50 cm-60 cm and the width of the ridge base being 70cm, applying base fertilizer while ditching, applying 750 kg/hm of sugarcane pesticide fertilizer containing 0.05 percent of dinotefuran2. 3. Seed arrangement, soil covering and film covering are carried out by adopting a sugarcane split type planter, the sugarcane is planted in a double-row manner of willow city 05/136, the spacing between two rows of sugarcane seeds is about 20cm, and the seeding amount is 10.5 t/hm2. 4. Applying 250 kg/hm of urea to the sugarcane banking machine in the seedling stage of the sugarcane in the middle ten days of the 4 th month2And at the same time of fertilizing, the grass is removed by a physical method. 5. In the elongation period of the sugarcane in the last 6 months, a deep-scarification, deep-ploughing, soil-breaking, furrowing and fertilization all-in-one machine is adopted for fertilizing and hilling, and 100 kg/hm of sugarcane pesticide fertilizer containing 0.05 percent of dinotefuran is applied2. 6. After the large hilling, herbicide is sprayed in time for soil sealing, 55 to 70 percent of metolachlor diuron 2700-2675L of weed stem leaves are added with water for directional spraying. Harvesting is carried out in late 12 months. 7. And (4) leveling and film covering the perennial root sugarcane by using a leveling machine in the middle ten days of the next 1 month. The field management in the later period is basically consistent with the new planted sugarcane. 8. In the mature period of the sugarcaneAnd (5) checking and accepting the sugarcane yield of the residential area, and simultaneously collecting soil and plant samples. The organic carbon content of the soil is measured by an oil bath heating potassium dichromate oxidation capacity measuring method, and the carbon content of the plants is measured by a TOC instrument. Collecting greenhouse gas samples by adopting a static box method, collecting greenhouse gas once a week after sugarcane is planted, continuously sampling for 7 days after fertilization or when rainfall is more than 20mm, and carrying out encrypted sampling and greenhouse gas determination chromatography. The sugarcane market price is calculated according to 520 Yuan.t, and the labor cost of the chemical fertilizer and pesticide mechanical tillage comprises the labor cost of land preparation, planting and ridging, a pesticide applying machine, fertilizer, pesticide and the middle part.|[0061] The conventional planting process comprises the following steps: the method comprises the steps of rotary tillage and soil preparation (the depth is about 17 cm) by a tractor, fertilizing, seed placing, soil covering and film covering by a planter, micro-planting by a small sugarcane banking machine in a seedling stage, fertilizing in an elongation stage and high banking (the banking height is 15-18 cm) by a large banking machine, chemical weeding and harvesting, leveling perennial sugarcane by a leveling machine in the next year, and finally ridge breaking, fertilizing and film covering (the later-stage field management is consistent with the new planted sugarcane).|[0062] Through the positioning monitoring of newly planted perennial roots for 2 years, compared with the habit of farmers, the sugarcane cultivation technical mode of the invention can increase the yield of sugarcane stalks by 16.13 t.hm in 2 years2The amplification is 15.67%; the labor cost of the mechanical tillage of the chemical fertilizer and the pesticide is reduced by 1538 yuan hm2(ii) a Increase of sugarcane yield value 9923 yuan hm2The net income is increased by 11461 yuan hm2(ii) a The biological carbon fixation amount of the sugarcane is increased by 274 t.hm2The amplification is 16.82 percent, the organic carbon of the soil is increased by 0.32 g/kg, and the soil CO is2And N2The cumulative total discharge amount of O is respectively reduced by 9.18 percent and 14.46 percent, and the cumulative total absorption amount of soil CH4 is increased by 29.56 percent; the lodging angle of the sugarcane is reduced by 87.90 percent. The technology reduces the production cost of the sugarcane, increases the yield of the sugarcane, improves the biological carbon fixation amount of the sugarcane and the organic matter content of soil, prevents the sugarcane from lodging, reduces the greenhouse gas emission of the soil of the sugarcane field, and has good economic benefit, ecological benefit and social benefit.|[0063] TABLE 1 analysis of sugarcane yield and ecological benefit under different cultivation|The above description is not intended to limit the present application, and the present application is not limited to the above examples, and those skilled in the art should understand that they can make various changes, modifications, additions or substitutions within the spirit and scope of the present application. Family Number|(100702247)|100702247|Abstract|(CN114680010 A)|The invention discloses a high - yield sugar cane planting method giving consideration to soil carbon sequestration and emission reduction in a red soil area . The method comprises the following steps : ( 1 ) performing crushing , stubble cleaning and linear pre - ditching on previous crop residues by adopting a stubble cleaning and pre - ditching machine ; ( 2 ) performing soil throwing type deep scarification , deep ploughing and soil crushing in the pre - opened furrow by adopting a field ploughing and managing all - in - one machine to form a planting furrow ; and ( 3 ) carrying out automatic seed placement , soil covering and film covering planting by adopting a sugarcane planting machine . And ( 4 ) fertilizing in a seedling stage and performing physical weeding and micro - hilling . And ( 5 ) carrying out fertilization and hilling operation by adopting a field plowing and managing all - in - one machine . ( 6 ) chemical weeding and harvesting . ( 7 ) leveling the ratoon sugarcane ridges and the sugarcane pockets by adopting a leveling machine , and throwing soil on the ridge surfaces to the two outer sides of the sugarcane pockets ; covering the perennial root sugarcane with a film for water retention and heat preservation after leveling ; and then managing and harvesting according to the steps ( 4 ) - ( 6 ) , and after each crop of sugarcane is harvested , crushing sugarcane leaves and returning the sugarcane leaves to the field . The application of the method realizes the purposes of carbon sequestration and emission reduction , lodging resistance and sugarcane yield and efficiency increase of soil in the sugarcane field . |CPC codes|(CN114680010 A)|A01B - 049/02/2 |A01B - 049/04 |A01B - 049/06/5 |A01C - 005/06/2 |A01G - 013/37 |A01G - 022/55 |IPC codes|(CN114680010 A)|A01B - 049/02 |A01B - 049/04 |A01B - 049/06 |A01C - 005/06 |A01G - 013/02 |A01G - 022/55 |Title|(CN114680010 A)|Sugarcane high - yield planting method giving consideration to soil carbon sequestration and emission reduction in red soil area | Other special machines A01B-049/02/2|A01B-049/04|A01B-049/06/5|A01C-005/06/2|A01G-013/37|A01G-022/55 A01B-049/02/2|A01B-049/04|A01B-049/06/5|A01C-005/06/2|A01G-013/37|A01G-022/55 A01B-049/02|A01B-049/04|A01B-049/06|A01C-005/06|A01G-013/02|A01G-022/55 A01B-049/02|A01B-049/04|A01B-049/06|A01C-005/06|A01G-013/02|A01G-022/55 CN121100607|CN118901318|CN119522666|CN116602182|CN115211268|CN119344032B|CN117957956B CN121100607 117014827 WHO=Examiner SELF=N CAT=A|CN118901318 112113726 WHO=Examiner SELF=N CAT=A|CN119522666 113580217 WHO=Examiner SELF=Y CAT=A|CN116602182 106176403 WHO=Examiner SELF=N CAT=A|CN115211268 102238834 WHO=Examiner SELF=N CAT=A|CN119344032B 113148714 WHO=Examiner SELF=N|CN117957956B 109629016 WHO=Examiner SELF=N CN109588253|CN112470849|CN110881389|CN111096207|CN110663492 CN109588253 84096820 WHO=Examiner SELF=Y CAT=X|CN112470849 93106701 WHO=Examiner SELF=Y CAT=A|CN110881389 87906909 WHO=Examiner SELF=Y CAT=A|CN111096207 88597682 WHO=Examiner SELF=Y CAT=A|CN110663492 87268328 WHO=Examiner SELF=Y CAT=A CN109588253; CN110663492; CN110881389; CN111096207; CN112470849 PENDING (CN114680010)|PENDING ALIVE (CN114680010)|ALIVE (CN114680010)|LEGAL DETAILS FOR CN114680010|Actual or expected expiration date=2042-05-18|Legal state=ALIVE|Status=PENDING|Event publication date=2022-05-18|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210538978|Application date=2022-05-18|Standardized application number=2022CN-0538978|Event publication date=2022-07-01|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114680010|Publication stage code=A|Publication date=2022-07-01|Standardized publication number=CN114680010|Event publication date=2022-07-01|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-07-19|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN114680010)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoReVD0dgrCW+lfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000063541385&ekey=2308&xpn=CN114680010&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=eJMLKdJz0LtzhNkGOe1LHJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN114680010)|CN (CN114680010)|NAME=GUANGXI ZHUANG AUTONOMOUS REGION ACADEMY OF AGRICULTURAL SCIENCES , COUNTRY=CN (CN114680010)|NAME=LAI GUANGYE;NANNING LAILAI PATENT AGENCY FIRM , REG=45118 (CN114680010)|NAME=HUANG JINSHENG|NAME=QIN LIPING|NAME=ZHOU LIUQIANG|NAME=YANG RUIQING|NAME=CENG YAN|NAME=ZHU XIAOHUI|NAME=TAN HONGWEI|NAME=HUANG XUEHUA|NAME=XIE RULIN|NAME=LÜ KUNMING|NAME=PENG JIAYU|NAME=LI ZHONGNING|NAME=LI ZHENGYOU 0 1 Titre: (CN114680010)|Sugarcane high-yield planting method giving consideration to soil carbon sequestration and emission reduction in red soil area Résumé: (CN114680010)|The invention discloses a high-yield sugar cane planting method giving consideration to soil carbon sequestration and emission reduction in a red soil area. The method comprises the following steps: (1) performing crushing, stubble cleaning and linear pre-ditching on previous crop residues by adopting a stubble cleaning and pre-ditching machine; (2) performing soil throwing type deep scarification, deep ploughing and soil crushing in the pre-opened furrow by adopting a field ploughing and managing all-in-one machine to form a planting furrow; and (3) carrying out automatic seed placement, soil covering and film covering planting by adopting a sugarcane planting machine. And (4) fertilizing in a seedling stage and performing physical weeding and micro-hilling. And (5) carrying out fertilization and hilling operation by adopting a field plowing and managing all-in-one machine. (6) chemical weeding and harvesting. (7) leveling the ratoon sugarcane ridges and the sugarcane pockets by adopting a leveling machine, and throwing soil on the ridge surfaces to the two outer sides of the sugarcane pockets; covering the perennial root sugarcane with a film for water retention and heat preservation after leveling; and then managing and harvesting according to the steps (4)-(6), and after each crop of sugarcane is harvested, crushing sugarcane leaves and returning the sugarcane leaves to the field. The application of the method realizes the purposes of carbon sequestration and emission reduction, lodging resistance and sugarcane yield and efficiency increase of soil in the sugarcane field. 19 Abstract gpt-4o-mini no The article focuses on a sugarcane planting method aimed at soil carbon sequestration and emission reduction, but it does not involve accelerated weathering of minerals or CO₂ capture through mineral carbonation.
21 CN202211017330 CN202211017330 CN115462205 102969094 CN115462205 A 2022-12-13 [CN115462205] 2022-08-23 2022-08-23 2022-12-13 (CN115462205)|2042-08-23 (CN115462205)|Method for improving carbon sequestration, sink increase and soil fertility of ecological restoration area of mine (CN115462205)|The invention relates to a method for improving carbon sequestration, sink increase and soil fertility of a mine ecological restoration area, and the mine ecological restoration area comprises a mine area soil composite modifier which comprises the following components in parts by weight: 10 parts of modified biochar, 40 parts of crushed plants, 2 parts of a complex microbial inoculant and 10 parts of fly ash; the invention further discloses a soil improvement method. The soil improvement method comprises the following steps that the mining area soil composite modifier and soil are mixed; the mining area soil is improved for 50-70 days by using the mining area soil composite modifier; the weight ratio of the soil to the modifier to the mixture is 100: (1-10), and the modifier and the mine soil are uniformly mixed and then directly cover the surface layer of the soil. The soil activator provided by the invention can effectively improve the soil structure, activate soil microorganisms, increase the soil fertility, improve the water and fertilizer retention capability of soil and promote the formation of soil aggregates, and the water and fertilizer retention duration is long. The soil conditioner can be used for improving mine soil with water and soil loss, and is low in cost and environment-friendly. ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY|PINGAN COAL MINING EXPLOITATION ENGINEERING TECHNOLOGY INSTITUTE (CN115462205)|ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN])|PINGAN COAL MINING EXPLOITATION ENGINEERING TECHNOLOGY INSTITUTE CO., LTD. CHEN XIAOYANG|ZHOU YUZHI|SU YONGDONG|CHEN YONGCHUN|AN SHIKAI|NIU JINGWEI|JIANG ZHIYANG (CN115462205)|CHEN XIAOYANG|ZHOU YUZHI|SU YONGDONG|CHEN YONGCHUN|AN SHIKAI|NIU JINGWEI|JIANG ZHIYANG (CN115462205)|ZHOU WEIMING;Wuhu Changqiang Patent Agency (Special General Partnership)|Reg. Nb: 34203 (CN115462205)|How to effectively improve poor soil and fully utilize limited land resources is a major problem which needs to be urgently solved in agricultural production, ecological construction and environmental protection.|The invention has the technical effects and advantages that: compared with the prior art, the method for improving the carbon fixation, sink increase and soil fertility of the ecological restoration area of the mine has the following advantages:|The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and drawings.| (CN115462205)|1. A method for improving carbon sequestration, sink increase and soil fertility in a mine ecological restoration area is characterized by comprising the following steps:the composite modifier comprises a mining area soil composite modifier and comprises the following components in parts by weight:10 parts of modified biochar, 40 parts of plant broken materials, 2 parts of a compound microbial inoculum and 10 parts of fly ash;the method for improving the soil comprises the following steps:mixing the composite amendment for the soil in the mining area with the soil;improving the mining area soil for 50-70 days by using the mining area soil composite improver;the soil and the modifying agent are mixed according to the weight ratio of 100 (1-10), and the modifying agent is mixed with the mine soil uniformly and then directly covered on the surface layer of the soil; after mixing, the soil humidity is kept between 40 and 70 percent, and water is poured once every 2 to 6 days.| (CN115462205)|The invention aims to provide a method for improving carbon sequestration, sink increase and soil fertility in a mine ecological restoration area, which can effectively improve a soil structure, activate soil microorganisms, increase the soil fertility, improve the water and fertilizer retention capacity of soil, promote the formation of soil aggregates, is low in cost and environment-friendly and solves the problems in the prior art in the background art. In order to achieve the purpose, the invention adopts the following technical scheme: the invention provides a mining area soil composite improver which comprises the following components: 10 parts of modified biochar, 40 parts of plant broken materials, 2 parts of a compound microbial inoculum and 10 parts of fly ash.|The invention relates to a method for improving carbon sequestration, sink increase and soil fertility in a mine ecological restoration area, which comprises a mining area soil composite modifier, and the mining area soil composite modifier comprises the following components in parts by weight: 10 parts of modified biochar, 40 parts of plant broken materials, 2 parts of a compound microbial inoculum and 10 parts of fly ash; the method for improving the soil comprises the following steps: mixing the composite amendment for the soil in the mining area with the soil; improving the mining area soil for 50-70 days by using the mining area soil composite improver; the soil and the modifying agent are mixed according to the weight ratio of 100 (1-10), and the modifying agent is mixed with the mine soil uniformly and then directly covered on the surface layer of the soil.|The invention relates to the technical field of soil improvement, in particular to an improvement method for improving soil fertility and carbon fixation and sink increase capacity of a mine ecological restoration area.| (CN115462205)|SOIL FERTILITY(100,27)|MINE ECOLOGICAL RESTORATION AREA(100,15)|CARBON SEQUESTRATION(100,14)|SINK(100,7)|SOIL COMPOSITE MODIFIER(100,3)|SOIL COMPOSITE IMPROVER(98,3)|COMPOUND MICROBIAL INOCULUM(77,7)|COMPOSITE AMENDMENT(67,2)|MINE SOIL(56,3)|SOIL MICROORGANISM(50,2)|GROUND(45,60)|COMPOSITE MODIFIER(43,1)|SOIL AGGREGATE(35,5)|FERTILIZER RETENTION CAPABILITY(35,1)|FERTILIZER RETENTION DURATION(35,1)|COLLECTING CROP STRAW(31,2)|COMPOSITE MICROBIAL INOCULUM(30,4)|EARTH ACTIVATOR(30,1)|SOIL HUMIDITY(29,3)|CULTURE SOIL(28,4)|FERTILIZER RETENTION CAPACITY(28,3)|TRICHODERMA HARZIANUM(26,6)|MOLYBDENUM ANTIMONY ANTICOLOR(26,2)|MINING AREA SOIL(25,2)|FLY ASH(24,27)|BACILLUS LICHENIFORMIS(24,6)|ECOLOGICAL CONSTRUCTION(24,1)|WHEAT STRAW(22,2)|SIEVE RESIDUE(22,1)|BACILLUS SUBTILIS(21,6)|CONSUMED FESO(21,2)|FORESTRY RESIDUE(21,2)|MODIFIED BIOCHAR(20,12)|TUBULAR FURNACE(20,1)|MINING AREA(19,19)|VIABLE COUNT(18,6)|SPECTROPHOTOMETER(18,4)|DIGESTION CONTAINER(18,2)|ENVIRONMENTAL PROTECTION(17,2)|LIMITED LAND RESOURCE(17,1)|HUNDRED MILLION(15,6)|TIGHTENING(15,1)|CARBON FIXATION(14,4)|DISCONTINUOUS MATERIAL(14,4)|WEIGHT RATIO(14,4)|ANAEROBIC CONDITION(14,2)|ECOLOGICAL RESTORATION AREA(14,2)|MINE(14,2)|SPECTROPHOTOMETRY(14,2)|GRAM(13,6)|MIXED INDICATOR(12,2)|MODIFIED SOLUTION(11,3)|CUVETTE(11,2)|DIGESTIVE JUICE(11,2)|FUNCTION SOIL(10,4)|TOTAL PHOSPHORUS CONTENT(10,4)|COMPLEX MICROBIAL INOCULUM(10,3)|CRUSHING(10,3)|JIG(10,3)|MUFFLE FURNACE(10,3)|AGRICULTURAL PRODUCTION(10,2)|COLOR COMPARISON(10,2)|CORN STRAW(10,2)|FUNCTION RICE STRAW(10,2)|IMPURITY(10,2)|VOLUME CONVERSION(10,2)|CARBONIZATION(10,1)|SOIL IMPROVEMENT(9,3)|MODIFICATION SOLUTION(9,2)|SHAKING(9,2)|ASSAY(9,1)|SURFACE LAYER(8,3)|TOTAL NITROGEN(8,3)|FERRIC CHLORIDE(8,2)|FERRIC IRON SOURCE(8,2)|FERRIC SULFATE(8,2)|GAUZE(8,2)|SILICATE MINERAL(8,2)|CLEAR LIQUID COLLECTION(8,1)|SOIL LOSS(8,1)|SOIL CONDITIONER(7,8)|WAVELENGTH FUNCTION(7,3)|FIXING NUTRIENT(7,2)|MOLAR CONCENTRATION(7,2)|NAOH(7,2)|ORGANIC MATTER CONTENT(7,2)|STRAIN ADAPTABILITY(7,2)|SOIL STRUCTURE(6,4)|PART FUNCTION(5,4)|STANDARD SOLUTION(5,3)|CREATIVE EFFORT(5,1)|STRAW DECOMPOSITION(5,1)|MICROORGANISM(4,3)|MODIFIER(4,3)|AIR BOX(4,2)|AMMONIUM NITROGEN(4,2)|CONTENT FUNCTION CALCIUM OXIDE(4,2)|POWER PLANT(4,2)|GEOGRAPHICAL ENVIRONMENT(4,1)|STRAW PLANT(4,1)|RATIO FUNCTION(3,5)|CONTENT FUNCTION ORGANIC MATTER(3,3)|DEGRADATION FUNCTION CELLULOSE(3,2)|FERTILIZER(3,2)| (CN115462205)|1. A method for improving carbon sequestration, sink increase and soil fertility in a mine ecological restoration area is characterized by comprising the following steps:|the composite modifier comprises a mining area soil composite modifier and comprises the following components in parts by weight:|10 parts of modified biochar, 40 parts of plant broken materials, 2 parts of a compound microbial inoculum and 10 parts of fly ash;|the method for improving the soil comprises the following steps:|mixing the composite amendment for the soil in the mining area with the soil;|improving the mining area soil for 50-70 days by using the mining area soil composite improver;|the soil and the modifying agent are mixed according to the weight ratio of 100 (1-10), and the modifying agent is mixed with the mine soil uniformly and then directly covered on the surface layer of the soil; after mixing, the soil humidity is kept between 40 and 70 percent, and water is poured once every 2 to 6 days.|2. The method for improving carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 1, wherein the method comprises the following steps: the modified biochar is prepared by the following steps: collecting crop straws and forestry residues to remove impurities, crushing the residues to be less than 3cm, carbonizing the residues for 2 to 3 hours under the anaerobic condition at the temperature of 450 to 550 ℃, recovering the temperature to be room temperature, completely soaking the biochar in a modification solution for 1 to 3 hours, and then putting the biochar into an air box at the temperature of 80 ℃ for drying to obtain the modified biochar.|3. The method for improving carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 2, wherein: the modified solution is Fe-containing 3+ The molar concentration of the solution is 0.2-0.4 mol/L.|4. The method for improving carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 3, wherein: fe of the modified solution 3+ The ferric iron source is ferric chloride or ferric sulfate.|5. The method for improving carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 4, wherein the method comprises the following steps: the straws need to be crushed before use, the crushed materials are one or more of rice straws, wheat straws and corn straws, and the carbonization process is carried out in a tubular furnace or a muffle furnace.|6. The method for improving the carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 1, characterized in that: the compound microbial inoculum comprises bacillus subtilis, bacillus licheniformis and trichoderma harzianum; the composite microbial inoculum is prepared by the following steps of inoculating bacillus subtilis, bacillus licheniformis and trichoderma harzianum in a ratio of 2:1:1.|7. the method for improving carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 6, wherein the method comprises the following steps: the effective viable count of the bacillus subtilis is more than or equal to 200 hundred million per gram, the effective viable count of the bacillus licheniformis is more than or equal to 100 hundred million per gram, and the effective viable count of the trichoderma harzianum is more than or equal to 100 hundred million per gram.|8. The method for improving carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 7, wherein: the fly ash is silicate mineral and comes from a power plant, the content of calcium oxide in the fly ash is 5.43 percent, the content is less than 10 percent, and the sieve residue of the fly ash is less than 12 percent, and the fly ash is naturally dried, crushed, ground and sieved by a sieve with 80 meshes.|9. The method for improving carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 8, wherein the method comprises the following steps: the method for measuring the content of organic matters in the soil before and after improvement by adopting a spectrophotometry comprises the following specific steps: drying, crushing and sieving the culture soil, taking 0.050 to 0.150g of soil and adding 0.4mol/L of K 2 Cr 2 O 7 And H 2 SO 4 Mixing the solution and preparing FeSO 4 And H 2 SO 4 The standard solution is digested at 150 deg.C for 30min, cooled and added with 0.1mol/L H 2 SO 4 Transferring part of the clear liquid into a cuvette for color comparison at 585nm according to consumed FeSO 4 The organic matter content in volume conversion.|10. The method for improving carbon sequestration, sink enhancement and soil fertility in the mine ecological restoration area according to claim 9, wherein the method comprises the following steps: the culture soil is air-dried, crushed and sieved when the total nitrogen and total phosphorus content in the soil is measured, 10-50 mg of soil and a digestion container are taken, and K is added 2 S 2 O 8 Mixing with NaOH to obtain digestive juice, covering, shaking, tightening cover with gauze, making 0-60 μ g nitrogen-phosphorus mixed standard solution, digesting at 120 deg.C under high pressure steam for 30min, cooling, collecting clear liquid, and performing NO treatment 3- -N and PO 3- -a P assay; NO 3- N selection at 220nm and 275nm wavelength detected by spectrophotometer, PO 3- Adding a molybdenum-antimony anti-color mixed indicator during P-test, developing for 30min at the temperature of 20-40 ℃, and detecting by a spectrophotometer at the wavelength of 700 nm. (CN115462205)|TECHNICAL FIELD|[0001] The invention relates to the technical field of soil improvement, in particular to an improvement method for improving soil fertility and carbon fixation and sink increase capacity of a mine ecological restoration area.|BACKGROUND ART|[0002] Soil is an important component of the geographical environment, is a material basis of agricultural production, and is a basic resource for ecological environment construction. In the process of production activities of human beings in mining areas, on one hand, the interference on the soil surface layer and vegetation in peripheral areas is easily caused, so that the structural function of soil is damaged, the carbon sink capacity of the soil is reduced, and effective soil aggregates cannot be formed to prevent the loss of nutrients, so that the fertility of the soil is reduced, and the land degradation is caused. On the other hand, the heavy metal content in the soil in the mining area is higher, which can destroy the capability of plants for absorbing other nutrient elements, influence the activity of microorganisms in the soil and cause the quantity reduction of the plants and the microorganisms. How to effectively improve poor soil and fully utilize limited land resources is a major problem which needs to be urgently solved in agricultural production, ecological construction and environmental protection. The biochar has high carbon content and strong stability, is a hotspot of research in the multidisciplinary field, and has great potential when applied to the agricultural field, so that a method for improving carbon fixation, sink increase and soil fertility in an ecological restoration area of a mine is provided to solve the problems in the prior art.|DISCLOSURE|Disclosure of Invention|[0003] The invention aims to provide a method for improving carbon sequestration, sink increase and soil fertility in a mine ecological restoration area, which can effectively improve a soil structure, activate soil microorganisms, increase the soil fertility, improve the water and fertilizer retention capacity of soil, promote the formation of soil aggregates, is low in cost and environment-friendly and solves the problems in the prior art in the background art.|[0004] In order to achieve the purpose, the invention adopts the following technical scheme:|[0005] the invention provides a mining area soil composite improver which comprises the following components: 10 parts of modified biochar, 40 parts of plant broken materials, 2 parts of a compound microbial inoculum and 10 parts of fly ash.|[0006] Preferably, the modified biochar is prepared by the following steps: collecting crop straws and forestry residues to remove impurities, crushing the residues to be less than 3cm, carbonizing the residues for 2 to 3 hours under the anaerobic condition at the temperature of 450 to 550 ℃, recovering the temperature to be room temperature, completely soaking the biochar in a modification solution for 1 to 3 hours, and then putting the biochar into an air box at the temperature of 80 ℃ for drying to obtain the modified biochar.|[0007] Wherein the modified solution contains Fe 3+ The molar concentration of the solution is 0.2-0.4 mol/L.|[0008] The above carbonization can be carried out in a tube furnace or a muffle furnace according to the present invention, and in the following examples of the present invention, the carbonization is carried out in a muffle furnace.|[0009] As preferred for providing Fe 3+ The ferric iron source is ferric chloride or ferric sulfate.|[0010] Preferably, the complex microbial inoculum comprises bacillus subtilis, bacillus licheniformis and trichoderma harzianum.|[0011] In order to further improve the straw decomposition efficiency, preferably, the strain ratio of the bacillus subtilis, the bacillus licheniformis and the trichoderma harzianum is 2:1:1.|[0012] preferably, the effective viable count of the bacillus subtilis is greater than or equal to 200 hundred million per gram, the effective viable count of the bacillus licheniformis is greater than or equal to 100 hundred million per gram, and the effective viable count of the trichoderma harzianum is greater than or equal to 100 hundred million per gram.|[0013] The straws need to be crushed before use, the crushed materials are one or more of rice straws, wheat straws and corn straws, and the crushing length can be determined by workers according to the field situation.|[0014] Preferably, the fly ash is a silicate mineral and originates from a power plant, the content of calcium oxide in the fly ash is 5.43 percent, the content is less than 10 percent, and the residue of the fly ash (passing through 45 mu m) is less than 12 percent, and the fly ash is naturally dried, crushed, ground and sieved by a 80-mesh sieve.|[0015] In addition, the invention also provides a soil improvement method, which comprises the step of mixing the soil improvement agent with soil.|[0016] The modifier is used for modifying the soil of the mining area for 50 to 70 days;|[0017] specifically, the soil and the modifying agent are mixed according to the weight ratio of 100 (1-10), and the modifying agent is uniformly mixed with the mine soil and then directly covered on the surface layer of the soil. After mixing, the soil humidity is kept between 40 and 70 percent, and water is poured once every 2 to 6 days.|[0018] Preferably, the weight ratio of the soil to the modifier is 100 (4-6), the soil humidity is kept between 50% and 60% after mixing, and water is poured once every 3 days.|[0019] Under the condition, the composite microbial inoculum has the strongest activity, and is beneficial to the degradation of crushed straw plants;|[0020] 1. organic carbon|[0021] The content of organic matters in the soil before and after improvement is measured by a spectrophotometry. The method comprises the following specific steps: drying, crushing and sieving the culture soil, taking 0.050 to 0.150g of soil and adding 0.4mol/L of K 2 Cr 2 O 7 And H 2 SO 4 Mixing the solution and preparing FeSO 4 And H 2 SO 4 The standard solution is digested at 150 ℃ for 30min, cooled and added with 0.1mol/L H 2 SO 4 Transferring part of the clear liquid into a cuvette for color comparison at 585nm according to consumed FeSO 4 The organic matter content in volume conversion.|[0022] 2. Determination of total nitrogen and total phosphorus content in soil|[0023] Drying the culture soil by wind, crushing and sieving, taking 10-50 mg of soil and a digestion container, adding K 2 S 2 O 8 Mixing with NaOH to obtain digestive juice, covering, shaking, fastening the cover with gauze, and making into the mixture 0-60 μ gDigesting nitrogen-phosphorus mixed standard liquid for 30min under the condition of high-pressure steam at 120 ℃, cooling, taking clear liquid, and carrying out NO treatment on the clear liquid 3- -N and PO 3- -P determination. NO 3- -N selection detected with a spectrophotometer at wavelengths of 220nm and 275nm, PO 3- Adding a molybdenum-antimony anti-color mixed indicator during P-test, developing for 30min at the temperature of 20-40 ℃, and detecting by a spectrophotometer at the wavelength of 700 nm.|[0024] The invention has the technical effects and advantages that: compared with the prior art, the method for improving the carbon fixation, sink increase and soil fertility of the ecological restoration area of the mine has the following advantages:|[0025] mixing the modified biochar, the plant broken parts, the composite microbial inoculum and the fly ash to generate a modifier;|[0026] (1) The modified biochar used in the invention has long lasting period, complete functions and low manufacturing cost; the pH value of the soil is increased, and the acid soil is improved; fixing nutrient elements and increasing the soil fertility; the heavy metal and organic pollutants are adsorbed and fixed, the activity of the heavy metal in the soil is reduced, and the formation of soil aggregates is promoted. Fe 3+ The fertilizer can be combined with organic acid in soil to fix ammonium nitrogen, prevent nitrogen loss and improve soil fertility;|[0027] (2) The compound microbial inoculum used by the invention has simple components, low cost, strong strain adaptability and activity, is harmless to human body, can accelerate the degradation of cellulose, hemicellulose, lignin and other components of the straw, inhibit the growth of harmful bacteria in soil, fix nitrogen and dissolve phosphorus, and quickly improve the soil fertility;|[0028] (3) The fly ash used in the invention has wide sources and low cost, can loosen soil, increases the air permeability of the soil, enables air and water to be more easily permeated, improves the soil permeability, improves the water and fertilizer retention capacity of the soil, has effective phosphorus and total phosphorus content obviously higher than that of the soil, can effectively improve the phosphorus content in the soil by properly applying the fly ash, can increase the number of water-stable aggregates larger than 1mm in the soil by applying the fly ash, and improves the soil structure;|[0029] (4) The raw materials of the invention are easy to obtain, the source is wide, the production cost is low, the preparation method is simple, and the mass production is easy.|[0030] Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and drawings.|DRAWINGS DESCRIPTION|[0031] FIG. 1 is a flow chart of the method for improving soil fertility and carbon sequestration capacity in the mine ecological restoration area.|INVENTION MODE|Detailed Description|[0032] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. The specific embodiments described herein are merely illustrative of the invention and do not delimit the invention. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.|[0033] The present invention provides the embodiments shown in the figures:|[0034] example 1|[0035] The method comprises the following steps of 1, uniformly mixing plant crushed materials, modified biochar, fly ash and a compound microbial agent according to a ratio of 1.|[0036] Example 2|[0037] The method comprises the following steps of 1, uniformly mixing plant crushed materials, modified biochar, fly ash and a compound microbial agent according to a ratio of 2.|[0038] Example 3|[0039] The method comprises the following steps of uniformly mixing plant crushed materials, modified biochar, fly ash and a compound microbial agent according to a ratio of 1.|[0040] Example 4|[0041] The method comprises the following steps of 1, uniformly mixing plant broken materials, common biochar, fly ash and a compound microbial agent according to a ratio of 2.|[0042] Comparative example 1|[0043] The soil in the mining area is improved and restored in a similar way to example 4, except that: no soil conditioner is added.|[0044] Comparative example 2|[0045] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises modified biochar.|[0046] Comparative example 3|[0047] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises plant broken substances and complex microbial inoculum.|[0048] Comparative example 4|[0049] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises fly ash.|[0050] Comparative example 5|[0051] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises modified biochar, plant broken substances and a compound microbial inoculum.|[0052] Comparative example 6|[0053] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises modified biochar and fly ash.|[0054] Comparative example 7|[0055] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises plant broken substances, a complex microbial inoculum and fly ash.|[0056] In conclusion, the modifying agent is prepared by mixing the modified biochar, the plant broken matter, the composite microbial inoculum and the fly ash;|[0057] (1) The modified biochar used in the invention has long lasting period, complete functions and low manufacturing cost; the pH value of the soil is increased, and the acid soil is improved; fixing nutrient elements and increasing the soil fertility; the heavy metal and organic pollutants are adsorbed and fixed, the activity of the heavy metal in the soil is reduced, and the formation of soil aggregates is promoted. Fe 3+ The fertilizer can be combined with organic acid in soil to fix ammonium nitrogen, prevent nitrogen loss and improve soil fertility;|[0058] (2) The compound microbial inoculum used by the invention has simple components, low cost, strong strain adaptability and activity, is harmless to human body, can accelerate the degradation of cellulose, hemicellulose, lignin and other components of the straw, inhibit the growth of harmful bacteria in soil, fix nitrogen and dissolve phosphorus, and quickly improve the soil fertility;|[0059] (3) The fly ash used in the invention has wide sources and low cost, can loosen soil, increases the air permeability of the soil, enables air and water to be more easily permeated, improves the soil permeability, improves the water and fertilizer retention capacity of the soil, has effective phosphorus and total phosphorus content obviously higher than that of the soil, can effectively improve the phosphorus content in the soil by properly applying the fly ash, can increase the number of water-stable aggregates larger than 1mm in the soil by applying the fly ash, and improves the soil structure;|[0060] (4) The raw materials of the invention are easy to obtain, the source is wide, the production cost is low, the preparation method is simple, the mass production is easy, and the conditioner prepared by the components according to the preparation method and the proportion can increase the carbon sink of soil, increase the activity of microorganisms and improve the soil fertility and has obvious synergistic effect.|[0061] The results of the tests in examples 1 to 4 and comparative examples 1 to 7 are as follows:|[0062] TABLE 1 soil improvement status|[0063] |[0064] |[0065] The experimental results in table 1 show that the soil conditioner can significantly improve the content of organic matters when applied to the soil in a mining area, and the data in examples 2 and 4 show that the modified biochar can effectively promote the content of the organic matters and the total nitrogen and total phosphorus to be improved, and the added straw broken substances, the microbial agent and the fly ash have synergistic effect, so that the carbon fixation and sequestration capacity and the soil fertility in the soil are improved together.|[0066] Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments or portions thereof without departing from the spirit and scope of the invention. (CN115462205)|TECHNICAL FIELD|[0001] The invention relates to the technical field of soil improvement, in particular to an improvement method for improving soil fertility and carbon fixation and sink increase capacity of a mine ecological restoration area.|BACKGROUND ART|[0002] Soil is an important component of the geographical environment, is a material basis of agricultural production, and is a basic resource for ecological environment construction. In the process of production activities of human beings in mining areas, on one hand, the interference on the soil surface layer and vegetation in peripheral areas is easily caused, so that the structural function of soil is damaged, the carbon sink capacity of the soil is reduced, and effective soil aggregates cannot be formed to prevent the loss of nutrients, so that the fertility of the soil is reduced, and the land degradation is caused. On the other hand, the heavy metal content in the soil in the mining area is higher, which can destroy the capability of plants for absorbing other nutrient elements, influence the activity of microorganisms in the soil and cause the quantity reduction of the plants and the microorganisms. How to effectively improve poor soil and fully utilize limited land resources is a major problem which needs to be urgently solved in agricultural production, ecological construction and environmental protection. The biochar has high carbon content and strong stability, is a hotspot of research in the multidisciplinary field, and has great potential when applied to the agricultural field, so that a method for improving carbon fixation, sink increase and soil fertility in an ecological restoration area of a mine is provided to solve the problems in the prior art.|DISCLOSURE|Disclosure of Invention|[0003] The invention aims to provide a method for improving carbon sequestration, sink increase and soil fertility in a mine ecological restoration area, which can effectively improve a soil structure, activate soil microorganisms, increase the soil fertility, improve the water and fertilizer retention capacity of soil, promote the formation of soil aggregates, is low in cost and environment-friendly and solves the problems in the prior art in the background art.|[0004] In order to achieve the purpose, the invention adopts the following technical scheme:|[0005] the invention provides a mining area soil composite improver which comprises the following components: 10 parts of modified biochar, 40 parts of plant broken materials, 2 parts of a compound microbial inoculum and 10 parts of fly ash.|[0006] Preferably, the modified biochar is prepared by the following steps: collecting crop straws and forestry residues to remove impurities, crushing the residues to be less than 3cm, carbonizing the residues for 2 to 3 hours under the anaerobic condition at the temperature of 450 to 550 ℃, recovering the temperature to be room temperature, completely soaking the biochar in a modification solution for 1 to 3 hours, and then putting the biochar into an air box at the temperature of 80 ℃ for drying to obtain the modified biochar.|[0007] Wherein the modified solution contains Fe 3+ The molar concentration of the solution is 0.2-0.4 mol/L.|[0008] The above carbonization can be carried out in a tube furnace or a muffle furnace according to the present invention, and in the following examples of the present invention, the carbonization is carried out in a muffle furnace.|[0009] As preferred for providing Fe 3+ The ferric iron source is ferric chloride or ferric sulfate.|[0010] Preferably, the complex microbial inoculum comprises bacillus subtilis, bacillus licheniformis and trichoderma harzianum.|[0011] In order to further improve the straw decomposition efficiency, preferably, the strain ratio of the bacillus subtilis, the bacillus licheniformis and the trichoderma harzianum is 2:1:1.|[0012] preferably, the effective viable count of the bacillus subtilis is greater than or equal to 200 hundred million per gram, the effective viable count of the bacillus licheniformis is greater than or equal to 100 hundred million per gram, and the effective viable count of the trichoderma harzianum is greater than or equal to 100 hundred million per gram.|[0013] The straws need to be crushed before use, the crushed materials are one or more of rice straws, wheat straws and corn straws, and the crushing length can be determined by workers according to the field situation.|[0014] Preferably, the fly ash is a silicate mineral and originates from a power plant, the content of calcium oxide in the fly ash is 5.43 percent, the content is less than 10 percent, and the residue of the fly ash (passing through 45 mu m) is less than 12 percent, and the fly ash is naturally dried, crushed, ground and sieved by a 80-mesh sieve.|[0015] In addition, the invention also provides a soil improvement method, which comprises the step of mixing the soil improvement agent with soil.|[0016] The modifier is used for modifying the soil of the mining area for 50 to 70 days;|[0017] specifically, the soil and the modifying agent are mixed according to the weight ratio of 100 (1-10), and the modifying agent is uniformly mixed with the mine soil and then directly covered on the surface layer of the soil. After mixing, the soil humidity is kept between 40 and 70 percent, and water is poured once every 2 to 6 days.|[0018] Preferably, the weight ratio of the soil to the modifier is 100 (4-6), the soil humidity is kept between 50% and 60% after mixing, and water is poured once every 3 days.|[0019] Under the condition, the composite microbial inoculum has the strongest activity, and is beneficial to the degradation of crushed straw plants;|[0020] 1. organic carbon|[0021] The content of organic matters in the soil before and after improvement is measured by a spectrophotometry. The method comprises the following specific steps: drying, crushing and sieving the culture soil, taking 0.050 to 0.150g of soil and adding 0.4mol/L of K 2 Cr 2 O 7 And H 2 SO 4 Mixing the solution and preparing FeSO 4 And H 2 SO 4 The standard solution is digested at 150 ℃ for 30min, cooled and added with 0.1mol/L H 2 SO 4 Transferring part of the clear liquid into a cuvette for color comparison at 585nm according to consumed FeSO 4 The organic matter content in volume conversion.|[0022] 2. Determination of total nitrogen and total phosphorus content in soil|[0023] Drying the culture soil by wind, crushing and sieving, taking 10-50 mg of soil and a digestion container, adding K 2 S 2 O 8 Mixing with NaOH to obtain digestive juice, covering, shaking, fastening the cover with gauze, and making into the mixture 0-60 μ gDigesting nitrogen-phosphorus mixed standard liquid for 30min under the condition of high-pressure steam at 120 ℃, cooling, taking clear liquid, and carrying out NO treatment on the clear liquid 3- -N and PO 3- -P determination. NO 3- -N selection detected with a spectrophotometer at wavelengths of 220nm and 275nm, PO 3- Adding a molybdenum-antimony anti-color mixed indicator during P-test, developing for 30min at the temperature of 20-40 ℃, and detecting by a spectrophotometer at the wavelength of 700 nm.|[0024] The invention has the technical effects and advantages that: compared with the prior art, the method for improving the carbon fixation, sink increase and soil fertility of the ecological restoration area of the mine has the following advantages:|[0025] mixing the modified biochar, the plant broken parts, the composite microbial inoculum and the fly ash to generate a modifier;|[0026] (1) The modified biochar used in the invention has long lasting period, complete functions and low manufacturing cost; the pH value of the soil is increased, and the acid soil is improved; fixing nutrient elements and increasing the soil fertility; the heavy metal and organic pollutants are adsorbed and fixed, the activity of the heavy metal in the soil is reduced, and the formation of soil aggregates is promoted. Fe 3+ The fertilizer can be combined with organic acid in soil to fix ammonium nitrogen, prevent nitrogen loss and improve soil fertility;|[0027] (2) The compound microbial inoculum used by the invention has simple components, low cost, strong strain adaptability and activity, is harmless to human body, can accelerate the degradation of cellulose, hemicellulose, lignin and other components of the straw, inhibit the growth of harmful bacteria in soil, fix nitrogen and dissolve phosphorus, and quickly improve the soil fertility;|[0028] (3) The fly ash used in the invention has wide sources and low cost, can loosen soil, increases the air permeability of the soil, enables air and water to be more easily permeated, improves the soil permeability, improves the water and fertilizer retention capacity of the soil, has effective phosphorus and total phosphorus content obviously higher than that of the soil, can effectively improve the phosphorus content in the soil by properly applying the fly ash, can increase the number of water-stable aggregates larger than 1mm in the soil by applying the fly ash, and improves the soil structure;|[0029] (4) The raw materials of the invention are easy to obtain, the source is wide, the production cost is low, the preparation method is simple, and the mass production is easy.|[0030] Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and drawings.|DRAWINGS DESCRIPTION|[0031] FIG. 1 is a flow chart of the method for improving soil fertility and carbon sequestration capacity in the mine ecological restoration area.|INVENTION MODE|Detailed Description|[0032] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. The specific embodiments described herein are merely illustrative of the invention and do not delimit the invention. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.|[0033] The present invention provides the embodiments shown in the figures:|[0034] example 1|[0035] The method comprises the following steps of 1, uniformly mixing plant crushed materials, modified biochar, fly ash and a compound microbial agent according to a ratio of 1.|[0036] Example 2|[0037] The method comprises the following steps of 1, uniformly mixing plant crushed materials, modified biochar, fly ash and a compound microbial agent according to a ratio of 2.|[0038] Example 3|[0039] The method comprises the following steps of uniformly mixing plant crushed materials, modified biochar, fly ash and a compound microbial agent according to a ratio of 1.|[0040] Example 4|[0041] The method comprises the following steps of 1, uniformly mixing plant broken materials, common biochar, fly ash and a compound microbial agent according to a ratio of 2.|[0042] Comparative example 1|[0043] The soil in the mining area is improved and restored in a similar way to example 4, except that: no soil conditioner is added.|[0044] Comparative example 2|[0045] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises modified biochar.|[0046] Comparative example 3|[0047] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises plant broken substances and complex microbial inoculum.|[0048] Comparative example 4|[0049] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises fly ash.|[0050] Comparative example 5|[0051] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises modified biochar, plant broken substances and a compound microbial inoculum.|[0052] Comparative example 6|[0053] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises modified biochar and fly ash.|[0054] Comparative example 7|[0055] The soil in the mining area is improved and restored in a similar way to example 4, except that: the soil conditioner only comprises plant broken substances, a complex microbial inoculum and fly ash.|[0056] In conclusion, the modifying agent is prepared by mixing the modified biochar, the plant broken matter, the composite microbial inoculum and the fly ash;|[0057] (1) The modified biochar used in the invention has long lasting period, complete functions and low manufacturing cost; the pH value of the soil is increased, and the acid soil is improved; fixing nutrient elements and increasing the soil fertility; the heavy metal and organic pollutants are adsorbed and fixed, the activity of the heavy metal in the soil is reduced, and the formation of soil aggregates is promoted. Fe 3+ The fertilizer can be combined with organic acid in soil to fix ammonium nitrogen, prevent nitrogen loss and improve soil fertility;|[0058] (2) The compound microbial inoculum used by the invention has simple components, low cost, strong strain adaptability and activity, is harmless to human body, can accelerate the degradation of cellulose, hemicellulose, lignin and other components of the straw, inhibit the growth of harmful bacteria in soil, fix nitrogen and dissolve phosphorus, and quickly improve the soil fertility;|[0059] (3) The fly ash used in the invention has wide sources and low cost, can loosen soil, increases the air permeability of the soil, enables air and water to be more easily permeated, improves the soil permeability, improves the water and fertilizer retention capacity of the soil, has effective phosphorus and total phosphorus content obviously higher than that of the soil, can effectively improve the phosphorus content in the soil by properly applying the fly ash, can increase the number of water-stable aggregates larger than 1mm in the soil by applying the fly ash, and improves the soil structure;|[0060] (4) The raw materials of the invention are easy to obtain, the source is wide, the production cost is low, the preparation method is simple, the mass production is easy, and the conditioner prepared by the components according to the preparation method and the proportion can increase the carbon sink of soil, increase the activity of microorganisms and improve the soil fertility and has obvious synergistic effect.|[0061] The results of the tests in examples 1 to 4 and comparative examples 1 to 7 are as follows:|[0062] TABLE 1 soil improvement status|[0063] |[0064] |[0065] The experimental results in table 1 show that the soil conditioner can significantly improve the content of organic matters when applied to the soil in a mining area, and the data in examples 2 and 4 show that the modified biochar can effectively promote the content of the organic matters and the total nitrogen and total phosphorus to be improved, and the added straw broken substances, the microbial agent and the fly ash have synergistic effect, so that the carbon fixation and sequestration capacity and the soil fertility in the soil are improved together.|[0066] Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments or portions thereof without departing from the spirit and scope of the invention. Family Number|(102969094)|102969094|Abstract|(CN115462205 A)|The invention relates to a method for improving carbon sequestration , sink increase and soil fertility of a mine ecological restoration area , and the mine ecological restoration area comprises a mine area soil composite modifier which comprises the following components in parts by weight : 10 parts of modified biochar , 40 parts of crushed plants , 2 parts of a complex microbial inoculant and 10 parts of fly ash ; the invention further discloses a soil improvement method . The soil improvement method comprises the following steps that the mining area soil composite modifier and soil are mixed ; the mining area soil is improved for 50-70 days by using the mining area soil composite modifier ; the weight ratio of the soil to the modifier to the mixture is 100 : ( 1-10 ) , and the modifier and the mine soil are uniformly mixed and then directly cover the surface layer of the soil . The soil activator provided by the invention can effectively improve the soil structure , activate soil microorganisms , increase the soil fertility , improve the water and fertilizer retention capability of soil and promote the formation of soil aggregates , and the water and fertilizer retention duration is long . The soil conditioner can be used for improving mine soil with water and soil loss , and is low in cost and environment - friendly . |CPC codes|(CN115462205 A)|A01B - 079/00 |IPC codes|(CN115462205 A)|A01B - 079/00 |Title|(CN115462205 A)|Method for improving carbon sequestration , sink increase and soil fertility of ecological restoration area of mine | Basic materials chemistry|Other special machines A01B-079/00|C09K-017/40|C09K-2101/00|C09K-2109/00 A01B-079/00|C09K-017/40|C09K-2101/00|C09K-2109/00 A01B-079/00|C09K-017/40|C09K-101/00|C09K-109/00 A01B-079/00|C09K-017/40|C09K-101/00|C09K-109/00 CN119608753|CN118525633|CN117546649 CN119608753 113770414 WHO=Examiner SELF=N CAT=Y|CN118525633 111163708 WHO=Examiner SELF=N CAT=A|CN117546649 108509002 WHO=Examiner SELF=N CAT=A PENDING (CN115462205)|PENDING ALIVE (CN115462205)|ALIVE (CN115462205)|LEGAL DETAILS FOR CN115462205|Actual or expected expiration date=2042-08-23|Legal state=ALIVE|Status=PENDING|Event publication date=2022-08-23|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211017330|Application date=2022-08-23|Standardized application number=2022CN-1017330|Event publication date=2022-12-13|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115462205|Publication stage code=A|Publication date=2022-12-13|Standardized publication number=CN115462205|Event publication date=2022-12-13|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-06-20|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN115462205)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQcT68NKeIkh1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000065803924&ekey=2319&xpn=CN115462205&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=NbqSKwNRLqSiyt0WsmKDGJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN115462205)|CN (CN115462205)|NAME=ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN115462205)|NAME=ZHOU WEIMING;Wuhu Changqiang Patent Agency (Special General Partnership) , REG=34203 (CN115462205)|NAME=CHEN XIAOYANG|NAME=ZHOU YUZHI|NAME=SU YONGDONG|NAME=CHEN YONGCHUN|NAME=AN SHIKAI|NAME=NIU JINGWEI|NAME=JIANG ZHIYANG 0 1 Titre: (CN115462205)|Method for improving carbon sequestration, sink increase and soil fertility of ecological restoration area of mine Résumé: (CN115462205)|The invention relates to a method for improving carbon sequestration, sink increase and soil fertility of a mine ecological restoration area, and the mine ecological restoration area comprises a mine area soil composite modifier which comprises the following components in parts by weight: 10 parts of modified biochar, 40 parts of crushed plants, 2 parts of a complex microbial inoculant and 10 parts of fly ash; the invention further discloses a soil improvement method. The soil improvement method comprises the following steps that the mining area soil composite modifier and soil are mixed; the mining area soil is improved for 50-70 days by using the mining area soil composite modifier; the weight ratio of the soil to the modifier to the mixture is 100: (1-10), and the modifier and the mine soil are uniformly mixed and then directly cover the surface layer of the soil. The soil activator provided by the invention can effectively improve the soil structure, activate soil microorganisms, increase the soil fertility, improve the water and fertilizer retention capability of soil and promote the formation of soil aggregates, and the water and fertilizer retention duration is long. The soil conditioner can be used for improving mine soil with water and soil loss, and is low in cost and environment-friendly. 15 Abstract gpt-4o-mini no The article focuses on soil improvement and fertility in a mine ecological restoration area, without explicit mention of accelerated weathering or mineral carbonation related to CO₂ capture.
22 CN202110672589 CN202110672589 CN113396708 96148517 CN113396708 A 2021-09-17 [CN113396708] 2021-06-17 2021-06-17 2021-09-17 (CN113396708)|2022-12-16 (CN113396708)|Carbon sequestration device for improving waxberry artificial forest and use method of carbon sequestration device (CN113396708)|The invention relates to the technical field of carbon sequestration of artificial forests, in particular to a carbon sequestration device for improving a waxberry artificial forest and a use method of the carbon sequestration device. The carbon sequestration device comprises movable plates which are symmetrically arranged; a movable frame is movably connected between the movable plates, a processing box is fixedly connected to the inner side wall of the movable frame, a rotating rod is rotationally connected to the interior of the processing box, a crushing cutter is fixedly connected to the rotating rod, the two ends of the rotating rod penetrate through the side wall of the processing box and are fixedly connected with gears, an outlet hole is formed in the lower end of the processing box, and a belt is in transmission connection with the interior of the movable frame and is located on the outer side of the processing box. According to the carbon sequestration device, the biomass carbon and soil organic carbon storage amount of a waxberry forest herbaceous layer is increased, meanwhile, the quality of waxberry fruits is obviously improved, the carbon sequestration capacity of a waxberry forest vegetation layer is obviously improved, and soil organic carbon loss is effectively prevented. ZHEJIANG A & F UNIVERSITY (CN113396708)|ZHEJIANG A&F UNIVERSITY ([CN]) ZHANG YONG|WANG ZENG|PENG XINYI|YANG SHUNING|CAI YANJIANG|WU JIASEN|HUANG YUJIE|WANG JIANWU|YE LIMIN (CN113396708)|ZHANG YONG|WANG ZENG|PENG XINYI|YANG SHUNING|CAI YANJIANG|WU JIASEN|HUANG YUJIE|WANG JIANWU|YE LIMIN (CN113396708)|PAN FANGHUA;ANHUA MEI SHAN PATENT BUSINESS OFFICE, ANHUA COUNTY|Reg. Nb: 43005 (CN113396708)|1. The utility model provides an improve fixed carbon device of artifical woods of red bayberry which characterized in that: comprises moving plates (1) which are symmetrically arranged; a movable frame (2) movably connected between the movable plates (1), a processing box (3) is fixedly connected on the inner side wall of the movable frame (2), a rotating rod (4) is connected in the rotating way of the processing box (3), a crushing knife (5) is fixedly connected on the rotating rod (4), two ends of the rotating rod (4) penetrate through the side wall of the processing box (3) and are fixedly connected with gears (46), the lower end of the processing box (3) is provided with an outlet hole (9), the movable frame (2) is connected with a belt (6) in a transmission way, the belt (6) is positioned at the outer side of the processing box (3), an annular soft plate (7) is fixedly connected above the belt (6), the side wall of the annular soft plate (7) opposite to the gear (46) is fixedly connected with a driving gear (8), and the driving gear (8) is meshed with the gear (46); the automatic feeding device is characterized in that a charging barrel (10) is movably connected to the lower portion of the belt (6), a discharging barrel (11) is movably connected to the bottom of the charging barrel (10), a discharging plate (12) is symmetrically and fixedly connected to the inner side wall of the charging barrel (10) in an inclined mode, a baffle (13) is elastically connected to the discharging plate (12), and a first push rod (14) is connected between the baffle (13) and the discharging barrel (11).|10. A use method of a carbon sequestration device for improving a waxberry artificial forest is characterized by comprising the following steps: the method comprises the following steps: the third motor (22) works to realize the rotation of the belt pulley (21), and the belt pulley (21) is matched with the belt (6), so that the belt (6) is moved in the rotation process of the belt pulley (21), and the movement of the annular soft plate (7) is realized, and as the driving teeth (8) are arranged on the annular soft plate (7), and the driving teeth (8) are matched with the gears (46), the rotating rod (4) rotates in the processing box (3), the rotation of the crushing knife (5) is realized in the rotation process of the rotating rod (4), and the chopping processing of straws placed in the processing box (3) is realized in the rotation process of the crushing knife (5); the fourth motor (25) works to realize the rotation of the charging barrel (10), the second push rod (36) moves in the rotating process of the charging barrel (10), when the second push rod (36) pushes the push block (39), the striker plate (38) moves through the push block (39), when one end of the striker plate (38) is not positioned in the outlet hole (9), the cut straws in the processing box (3) fall on the screening plate (40) from the outlet hole (9), the straws with smaller sizes fall below the screening plate (40) from a gap between the movable cutting knife (43) and the fixed cutting knife (41), the straws with larger sizes are positioned on the screening plate (40), the second pneumatic telescopic rod (33) works to realize the downward movement of the connecting plate (35), and then the fifth motor (34) works to realize the rotation of the connecting plate (35), so that the second push rod (36) is positioned on the upper surface of the screening plate (40), the third pneumatic telescopic rod works to realize that the second push rod (36) moves in the horizontal direction, the movable plate (42) is pushed to move when the second push rod (36) moves in the horizontal direction, straws on the screening plate (40) fall between the fixed cutting knife (41) and the movable cutting knife (43) in the moving process of the movable plate (42), and meanwhile, the movable cutting knife (43) moves in the moving process of the movable plate (42), and the straws are cut under the action of the movable cutting knife (43) and the fixed cutting knife (41); the charging barrel (10) moves downwards when the first pneumatic telescopic rod (26) works, the charging barrel (11) moves downwards in the process of moving downwards of the charging barrel (10), when the bottom of the discharging barrel (11) is in contact with the ground of a waxberry forest land, the discharging barrel (11) moves upwards, the baffle (13) moves through the first push rod (14) when the discharging barrel (11) moves upwards, the straw conveniently located on the discharging plate (12) drops in the discharging barrel (11), and the straw drops on the waxberry forest land ground through the discharging hole (32) of the discharging barrel (11).| (CN113396708)|Aiming at the problems in the prior art, the invention provides a carbon fixation device for improving a waxberry artificial forest and a using method thereof.|The invention relates to the technical field of carbon sequestration of artificial forests, in particular to a carbon sequestration device for improving a waxberry artificial forest and a using method thereof, wherein the carbon sequestration device comprises moving plates which are symmetrically arranged; the movable frame is movably connected between the movable plates, the processing box is fixedly connected to the inner side wall of the movable frame, the rotating rod is connected to the processing box in a rotating mode, the crushing cutter is fixedly connected to the rotating rod, two ends of the rotating rod penetrate through the side wall of the processing box and are fixedly connected with the gear, the lower end of the processing box is provided with the outlet hole, the belt is connected to the movable frame in a transmission mode and is located on the outer side of the processing box. The invention relates to the technical field of carbon sequestration of artificial forests, in particular to a carbon sequestration device for improving a waxberry artificial forest and a using method thereof.| (CN113396708)|CARBON SEQUESTRATION(100,17)|BAYBERRY ARTIFICIAL FOREST(100,8)|WAX(100,8)|ARTIFICIAL FOREST(100,7)|BERRY ARTIFICIAL FOREST(100,6)|WAX BERRY ARTIFICIAL FOREST(100,6)|CARBON FIXATION(100,5)|RED BAYBERRY(100,2)|ARTIFICAL WOOD(100,1)|FIXED CARBON(100,1)|RED BAYBERRY ARTIFICAL WOOD(100,1)|CHARGE BARREL(68,37)|BARREL DISCHARGE(63,19)|PNEUMATIC TELESCOPIC ROD(56,33)|CRUSHING KNIFE(46,6)|ARTIFICIAL FOREST CARBON SEQUESTRATION(46,2)|MOVEABLE CUTTING KNIFE(40,22)|PROCESSING BOX(39,25)|ROTATING ROD(35,16)|SCREEN PLATE(35,12)|BELT PULLEY(33,15)|OUTLET HOLE(28,24)|DRIVING GEAR(27,2)|MOVEABLE FRAME(26,20)|CRUSHING KNIFE ROTATION(26,2)|STRAW(24,41)|DISCHARGE PLATE(24,8)|WAX BERRY GROUND(24,4)|MOVEABLE PLATE(23,36)|FIXED CUTTING KNIFE(23,20)|ANNULAR SOFT PLATE(23,12)|CHARGING BARREL ROTATION(22,2)|DRIVING TOOTH(21,8)|CRUSHING CUTTER(21,3)|EJECTOR PAD(21,2)|DISCHARGE(21,1)|PUSH ROD(20,38)|WAX BERRY(19,6)|STRAW DROP(18,4)|BAFFLE(17,12)|ANNULAR SPACING GROOVE(17,2)|BLOCKING ROD(16,15)|SLIDING GROOVE(16,9)|DISCHARGING BARREL BOTTOM(16,2)|MODE INCLINATION(16,1)|PUSH BLOCK(14,5)|CUT STRAW(14,4)|MOVEABLE CUTTING KNIFE ACTION(14,4)|CHARGING BARREL BOTTOM(14,3)|CHOPPING(14,2)|FIXED ROD(13,4)|UNIVERSAL WHEEL(12,5)|DISCHARGE BARREL(12,3)|SWING JOINT(11,2)|STRIKER PLATE(10,11)|MOVING PLATE(10,9)|CHARGING BARREL ROTATING(10,2)|FIXING BOLT(9,4)|DOWNWARD MOVEMENT(8,6)|HORIZONTAL DIRECTION(8,5)|STOPPER(8,5)|WATER INLET(8,5)|ANNULAR SOFT PLATE MOVEMENT(8,3)|SOIL TURNING(8,3)|TRANSMISSION MODE(8,3)|ROTATING MODE(8,2)|ACTIVITY FRAME INSIDE WALL(7,4)|CHARGING BAMBOO(7,4)|DISCHARGE HOLE(7,3)|HOLDING TANK(7,2)|DRIVING SHAFT(6,13)|ACCOMMODATING GROOVE(6,4)|BLOCKING BLOCK(6,3)|OUTSIDE WALL(6,1)|PHASE CONNECTING ROD(5,12)|MOVING(5,11)|WATER OUTLET(5,6)|WAX GROUND(5,6)|THREADED CONNECTION(5,4)|BELT PULLEY COOPERATEE(5,1)|HOLE LATERAL WALL(5,1)|SLIDING BLOCK(4,11)|THREADED ROD(4,9)|ROTATING(4,5)|ANNULAR SOFT BOARD(4,4)|CHARGING ROTATION(4,3)|SHREDDING EQUIPMENT(4,2)|ARTIFICIAL RED BAYBERRY FOREST(4,1)|BAMBOO BREAKAGE DROP(4,1)|BAYBERRY FRUIT QUALITY(4,1)|RED BAYBERRY FOREST LAND(4,1)|WAX WATERING TREATMENT(4,1)|MOVEABLE PLATE MOVING(3,10)|DWANG(3,4)|OUTER SIDE(3,4)|ANNULAR LIMITING GROOVE(3,3)|ANNULAR SPACE(3,3)|DRIVE TOOTH(3,3)|PROCESSING BOX END(3,3)|PROCESSING BOX OUTER SIDE(3,3)|WATER CHARGE(3,3)|WOODLAND(3,3)|WORKER(3,3)|FIXED CONNECTION(3,2)|SCREENING PLATE UPPER SURFACE(3,2)|ARTIFICIAL WAX(3,1)|BAYBERRY LAYER BIOMASS CARBON(3,1)|CHARGING BARREL INTERIOR(3,1)|CUTTING STRAW(3,1)|DEAD LEVER(3,1)|DRIVING TOOTH MATCHING(3,1)|FOREST FUNCTION EXERTION(3,1)|PNEUMATIC TELESCOPIC ROD WORK(3,1)|SINKING PHENOMENON(3,1)|SOIL SACK(3,1)|SUBTROPICAL ZONE(3,1)|SUNKEN HOLE GROUND(3,1)|WAX VEGETABLE LAYER(3,1)|MOTOR WORK(2,5)|PROCESSING BOX SIDE WALL(2,3)|CHARGING MOVEMENT(2,2)|WAX CARBON FIXING CAPACITY(2,2)|BAYBERRY CARBON FIXATION ABILITY(2,1)|BROKEN SWORD(2,1)|CONVEYING EQUIPMENT(2,1)|DEMOUNTING(2,1)|DISCHARGING HOLE(2,1)|GLOBAL CARBON TRADING(2,1)|MIDDLE SCREEN PANEL(2,1)|WAX HERBACEOUS LAYER(2,1)| (CN113396708)|1. The invention provides an improve fixed carbon device of artifical woods of red bayberry which characterized in that: comprises moving plates (1) which are symmetrically arranged;|a movable frame (2) movably connected between the movable plates (1), a processing box (3) is fixedly connected on the inner side wall of the movable frame (2), a rotating rod (4) is connected in the rotating way of the processing box (3), a crushing knife (5) is fixedly connected on the rotating rod (4), two ends of the rotating rod (4) penetrate through the side wall of the processing box (3) and are fixedly connected with gears (46), the lower end of the processing box (3) is provided with an outlet hole (9), the movable frame (2) is connected with a belt (6) in a transmission way, the belt (6) is positioned at the outer side of the processing box (3), an annular soft plate (7) is fixedly connected above the belt (6), the side wall of the annular soft plate (7) opposite to the gear (46) is fixedly connected with a driving gear (8), and the driving gear (8) is meshed with the gear (46);|the automatic feeding device is characterized in that a charging barrel (10) is movably connected to the lower portion of the belt (6), a discharging barrel (11) is movably connected to the bottom of the charging barrel (10), a discharging plate (12) is symmetrically and fixedly connected to the inner side wall of the charging barrel (10) in an inclined mode, a baffle (13) is elastically connected to the discharging plate (12), and a first push rod (14) is connected between the baffle (13) and the discharging barrel (11).|2. The device of claim 1, wherein the carbon sequestration for the bayberry artificial forest is enhanced by: the bottom end of the moving plate (1) is provided with a universal wheel (15);|the movable plate is characterized in that a sliding groove (16) is formed in the movable plate (1), a sliding block (17) is connected in the sliding groove (16), a first motor (18) is fixedly connected in the sliding groove (16), a threaded rod (19) is fixedly connected to the driving shaft of the first motor (18), the threaded rod (19) is in threaded connection with the sliding block (17), a second motor (20) is fixedly connected to the sliding block (17), and the driving shaft of the second motor (20) is fixedly connected with the movable frame (2).|3. The device of claim 1, wherein the carbon sequestration for the bayberry artificial forest is enhanced by: the inside wall of activity frame (2) rotates and is connected with belt pulley (21), belt (6) transmission is connected between two belt pulleys (21), fixedly connected with third motor (22) on activity frame (2), third motor (22) and one of them belt pulley (21) fixed connection.|4. The device of claim 1, wherein the carbon sequestration for the bayberry artificial forest is enhanced by: annular spacing groove (23) have been seted up on the inside wall of activity frame (2), fixedly connected with stopper (24) on the outside wall of belt (6), stopper (24) swing joint is in annular spacing groove (23).|5. The device of claim 1, wherein the carbon sequestration for the bayberry artificial forest is enhanced by: the lower end of the belt (6) is fixedly connected with a fourth motor (25), a driving shaft of the fourth motor (25) is fixedly connected with a first pneumatic telescopic rod (26), and the movable end of the first pneumatic telescopic rod (26) is fixedly connected with the charging barrel (10);|the discharging plate (12) is fixedly connected with a first spring (27), and one end of the first spring (27) is fixedly connected to the baffle plate (13).|6. The device of claim 1, wherein the carbon sequestration for the bayberry artificial forest is enhanced by: a water charging box (28) is fixedly connected to the inner side wall of the charging barrel (10), water inlet holes are formed in the side walls of the water charging box (28) and the charging barrel (10), a blocking block (29) is connected to the water inlet holes in a threaded manner, water outlet holes are formed in the side walls of the water charging box (28) and the charging barrel (10), a blocking rod (30) is movably connected to each water outlet hole, the lower end of the blocking rod (30) is fixedly connected with a phase connecting rod (31), and the phase connecting rod (31) is fixedly connected with the discharging barrel (11);|the area value of the cross section of the phase connecting rod (31) is smaller than that of the cross section of the blocking rod (30);|the lower end of the discharge barrel (11) is provided with a discharge hole (32).|7. The device of claim 1, wherein the carbon sequestration for the bayberry artificial forest is enhanced by: a second pneumatic telescopic rod (33) is fixedly connected to the inner side wall of the charging barrel (10), a fifth motor (34) is fixedly connected to the movable end of the second pneumatic telescopic rod (33), a connecting plate (35) is connected to a driving shaft of the fifth motor (34), and a second push rod (36) is fixedly connected to the connecting plate (35);|the holding tank has been seted up on the lateral wall of the hole (9) of processing box (3), fixedly connected with second spring (37) in the holding tank, fixedly connected with striker plate (38) on second spring (37), fixedly connected with ejector pad (39) on striker plate (38), ejector pad (39) are corresponding with second push rod (36).|8. The device of claim 7, wherein the carbon sequestration for the bayberry artificial forest is enhanced by: a screening plate (40) is fixedly connected to the inner side wall of the charging barrel (10), an outlet hole is formed in the screening plate (40), a fixed cutting knife (41) is fixedly connected to the side wall of the outlet hole, a movable plate (42) is movably connected to the inside of the outlet hole, a movable cutting knife (43) is fixedly connected to the movable plate (42), the movable cutting knife (43) is matched with the fixed cutting knife (41), and the movable plate (42) corresponds to the second push rod (36);|and a third spring (44) is fixedly connected to the movable plate (42), and one end of the third spring (44) is fixedly connected to the side wall of the outlet hole.|9. The device of claim 1, wherein the carbon sequestration for the bayberry artificial forest is enhanced by: the upper end of the belt (6) is connected with a fixing rod (47) through a fixing bolt (48), and a soil turning plate (45) is fixedly connected onto the fixing rod (47).|10. A use method of a carbon sequestration device for improving a waxberry artificial forest is characterized by comprising the following steps: the method comprises the following steps:|the third motor (22) works to realize the rotation of the belt pulley (21), and the belt pulley (21) is matched with the belt (6), so that the belt (6) is moved in the rotation process of the belt pulley (21), and the movement of the annular soft plate (7) is realized, and as the driving teeth (8) are arranged on the annular soft plate (7), and the driving teeth (8) are matched with the gears (46), the rotating rod (4) rotates in the processing box (3), the rotation of the crushing knife (5) is realized in the rotation process of the rotating rod (4), and the chopping processing of straws placed in the processing box (3) is realized in the rotation process of the crushing knife (5);|the fourth motor (25) works to realize the rotation of the charging barrel (10), the second push rod (36) moves in the rotating process of the charging barrel (10), when the second push rod (36) pushes the push block (39), the striker plate (38) moves through the push block (39), when one end of the striker plate (38) is not positioned in the outlet hole (9), the cut straws in the processing box (3) fall on the screening plate (40) from the outlet hole (9), the straws with smaller sizes fall below the screening plate (40) from a gap between the movable cutting knife (43) and the fixed cutting knife (41), the straws with larger sizes are positioned on the screening plate (40), the second pneumatic telescopic rod (33) works to realize the downward movement of the connecting plate (35), and then the fifth motor (34) works to realize the rotation of the connecting plate (35), so that the second push rod (36) is positioned on the upper surface of the screening plate (40), the third pneumatic telescopic rod works to realize that the second push rod (36) moves in the horizontal direction, the movable plate (42) is pushed to move when the second push rod (36) moves in the horizontal direction, straws on the screening plate (40) fall between the fixed cutting knife (41) and the movable cutting knife (43) in the moving process of the movable plate (42), and meanwhile, the movable cutting knife (43) moves in the moving process of the movable plate (42), and the straws are cut under the action of the movable cutting knife (43) and the fixed cutting knife (41);|the charging barrel (10) moves downwards when the first pneumatic telescopic rod (26) works, the charging barrel (11) moves downwards in the process of moving downwards of the charging barrel (10), when the bottom of the discharging barrel (11) is in contact with the ground of a waxberry forest land, the discharging barrel (11) moves upwards, the baffle (13) moves through the first push rod (14) when the discharging barrel (11) moves upwards, the straw conveniently located on the discharging plate (12) drops in the discharging barrel (11), and the straw drops on the waxberry forest land ground through the discharging hole (32) of the discharging barrel (11). (CN113396708)|TECHNICAL FIELD|[0001] The invention relates to the technical field of carbon sequestration of artificial forests, in particular to a carbon sequestration device for improving a waxberry artificial forest and a using method thereof.|BACKGROUND ART|[0002] The waxberry is an important fruit tree in subtropical zones in China, the planting area reaches 150 million hectares, the fruit has unique flavor and high nutritive value, and the waxberry is popular among people. However, due to excessive management, the shrub layer and the herbaceous layer under the tree are completely disappeared, water and soil loss is serious, the carbon fixing capacity of the vegetable layer under the waxberry tree is obviously reduced, organic carbon in the soil is lost, and the carbon fixing capacity of the artificial waxberry forest and the exertion of other forest functions are seriously damaged. Therefore, the key technology for improving the carbon fixing capacity of the waxberry artificial forest has very important significance for providing technical storage for responding to global carbon trading and improving the carbon fixing capacity of the waxberry artificial forest to the maximum extent.|[0003] However, in the existing carbon sequestration method for the artificial red bayberry forest, before the straws are laid on the ground of the red bayberry forest land, in order to better improve the biomass carbon and the soil organic carbon storage amount, the straws need to be shredded by additional shredding equipment and then laid on the red bayberry forest land by conveying equipment, and this method needs to be operated by a worker in advance, prolongs the treatment time, and when the straws are shredded by additional shredding equipment in other places, the straws are easy to splash after being shredded, thereby causing the waste of straw raw materials.|DISCLOSURE|Disclosure of Invention|[0004] Aiming at the problems in the prior art, the invention provides a carbon fixation device for improving a waxberry artificial forest and a using method thereof.|[0005] The technical scheme adopted by the invention for solving the technical problems is as follows: a carbon fixation device for improving the waxberry artificial forest comprises symmetrically arranged moving plates;|[0006] the movable frame is movably connected between the movable plates, a processing box is fixedly connected to the inner side wall of the movable frame, a rotating rod is connected to the inner rotation of the processing box, a crushing cutter is fixedly connected to the rotating rod, two ends of the rotating rod penetrate through the side wall of the processing box and are fixedly connected with gears, an outlet hole is formed in the lower end of the processing box, a belt is connected to the movable frame in a transmission mode and is located on the outer side of the processing box, an annular soft plate is fixedly connected to the upper portion of the belt, driving teeth are fixedly connected to the side wall of the annular soft plate, opposite to the gears, and the driving teeth are meshed with the gears;|[0007] the feeding device is characterized in that a charging barrel is movably connected below the belt, a discharging barrel is movably connected at the bottom of the charging barrel, discharging plates are symmetrically, obliquely and fixedly connected to the inner side wall of the charging barrel, a baffle is elastically connected to the discharging plates, and a first push rod is connected between the baffle and the discharging barrel.|[0008] The bottom end of the moving plate is provided with a universal wheel;|[0009] the movable plate is provided with a sliding groove, a sliding block is connected in the sliding groove in a sliding mode, a first motor is fixedly connected in the sliding groove, a threaded rod is fixedly connected to the driving shaft of the first motor, the threaded rod is in threaded connection with the sliding block, a second motor is fixedly connected to the sliding block, and the driving shaft of the second motor is fixedly connected with the movable frame.|[0010] The inside wall of activity frame rotates and is connected with the belt pulley, belt transmission connects between two belt pulleys, fixedly connected with third motor on the activity frame, third motor and one of them belt pulley fixed connection.|[0011] An annular limiting groove is formed in the inner side wall of the movable frame, a limiting block is fixedly connected to the outer side wall of the belt, and the limiting block is movably connected to the annular limiting groove.|[0012] The lower end of the belt is fixedly connected with a fourth motor, a driving shaft of the fourth motor is fixedly connected with a first pneumatic telescopic rod, and the movable end of the first pneumatic telescopic rod is fixedly connected with the charging barrel;|[0013] the stripper plate is fixedly connected with a first spring, and one end of the first spring is fixedly connected to the baffle plate.|[0014] The inner side wall of the charging barrel is fixedly connected with a water charging tank, the side walls of the water charging tank and the charging barrel are both provided with water inlet holes, the water inlet holes are in threaded connection with a blocking block, the side walls of the water charging tank and the charging barrel are both provided with water outlet holes, blocking rods are movably connected in the water outlet holes, the lower ends of the blocking rods are fixedly connected with phase connecting rods, and the phase connecting rods are fixedly connected with the discharging barrel;|[0015] the area value of the cross section of the phase connecting rod is smaller than that of the cross section of the blocking rod;|[0016] the lower end of the discharge barrel is provided with a discharge hole.|[0017] A second pneumatic telescopic rod is fixedly connected to the inner side wall of the charging barrel, a fifth motor is fixedly connected to the movable end of the second pneumatic telescopic rod, a driving shaft of the fifth motor is connected with a connecting plate, and a second push rod is fixedly connected to the connecting plate;|[0018] the accommodating groove is formed in the outlet side wall of the processing box, a second spring is fixedly connected in the accommodating groove, a material baffle plate is fixedly connected to the second spring, a pushing block is fixedly connected to the material baffle plate, and the pushing block corresponds to the second push rod.|[0019] A screening plate is fixedly connected to the inner side wall of the charging barrel, an outlet hole is formed in the screening plate, a fixed cutting knife is fixedly connected to the side wall of the outlet hole, a movable plate is movably connected to the outlet hole, a movable cutting knife is fixedly connected to the movable plate, the movable cutting knife is matched with the fixed cutting knife, and the movable plate corresponds to the second push rod;|[0020] the movable plate is fixedly connected with a third spring, and one end of the third spring is fixedly connected to the side wall of the outlet hole.|[0021] The upper end of the belt is connected with a fixed rod through a fixed bolt, and the fixed rod is fixedly connected with a soil turning plate.|[0022] A use method of a carbon sequestration device for improving a waxberry artificial forest comprises the following steps:|[0023] the third motor works to realize the rotation of the belt pulley, and the belt pulley is matched with the belt, so that the belt is moved in the rotation process of the belt pulley, and the movement of the annular soft plate is realized;|[0024] the fourth motor works to realize the rotation of the charging barrel, the second push rod moves in the rotating process of the charging barrel, when the second push rod pushes the push block, the baffle plate moves through the push block, when one end of the baffle plate is not positioned in the outlet hole, the cut straws in the processing box fall on the screening plate from the outlet hole, the straws with smaller size fall to the lower part of the screening plate from a gap between the movable cutting knife and the fixed cutting knife, the straws with larger size are positioned on the screening plate, the second pneumatic telescopic rod works to realize the downward movement of the connecting plate, then the fifth motor works to realize the rotation of the connecting plate, so that the second push rod is positioned on the upper surface of the screening plate, the third pneumatic telescopic rod works to realize the movement of the second push rod in the horizontal direction, when the second push rod moves in the horizontal direction, the movable plate moves, the straws on the screening plate fall between the fixed cutting knife and the movable cutting knife in the moving process of the movable plate, meanwhile, the movable cutting knife is moved in the moving process of the movable plate, and the movable cutting knife and the fixed cutting knife are used for cutting straws;|[0025] the charging barrel moves downwards when the first pneumatic telescopic rod works, the charging barrel moves downwards in the process of moving downwards of the charging barrel, when the bottom of the discharging barrel is in contact with the ground of a waxberry forest land, the discharging barrel moves upwards, the baffle moves through the first push rod when the discharging barrel moves upwards, straw on the discharging plate drops in the discharging barrel conveniently, and then the straw drops on the ground of the waxberry forest land through the discharging hole of the discharging barrel.|[0026] The invention has the beneficial effects that:|[0027] through setting up the section of thick bamboo of charging in the below of belt, the straw after will handling a section of thick bamboo breakage drops in the section of thick bamboo of charging, the belt pulley rotation is realized in third motor work, because the belt pulley cooperatees with the belt, consequently, it removes to realize the belt at belt pulley pivoted in-process, the in-process that removes at the belt realizes the section of thick bamboo of charging and removes, thereby be convenient for be equipped with the straw in the section of thick bamboo of charging and cover subaerial at the bayberry forest land, this layer biomass carbon of bayberry forest grass and soil organic carbon storage have been improved, the quality of bayberry fruit has also obviously been improved simultaneously, the carbon fixation ability of bayberry forest vegetable layer obviously improves, effectively prevent soil organic carbon loss.|[0028] Through setting up the dwang in the processing box to be provided with broken sword on the dwang, because drive tooth and gear on the annular soft board cooperate, consequently realize gear revolve through the annular soft board when the belt removes, realize the dwang at gear revolve's in-process and rotate, thereby realize the processing of cutting up of straw to being located the processing box.|[0029] The water tank is arranged in the charging barrel, so that the waxberry forest land is watered conveniently. In the process of upward movement of the discharge barrel, the upward movement of the blocking rod is realized through the connecting rod, and the area value of the cross section of the connecting rod is smaller than that of the cross section of the blocking rod, so that water in the water containing tank flows out through the water outlet hole, and the watering treatment of the waxberry forest land is realized.|[0030] The method improves the biomass carbon of the herbaceous layer of the waxberry forest and the organic carbon storage amount of the soil, obviously improves the quality of waxberry fruits, obviously improves the carbon fixation capacity of the vegetable layer of the waxberry forest, and effectively prevents the organic carbon loss of the soil.|DRAWINGS DESCRIPTION|[0031] The invention is further illustrated with reference to the following figures and examples.|[0032] FIG. 1 is a schematic view of the present invention;|[0033] FIG. 2 is an enlarged view of a portion of FIG. 1 at A;|[0034] FIG. 3 is a schematic view of the interior of the charging barrel and the discharging barrel of the present invention;|[0035] FIG. 4 is an enlarged view of a portion of FIG. 3 at B;|[0036] FIG. 5 is a schematic view of a middle process cartridge according to the present invention;|[0037] FIG. 6 is a cross-sectional view taken along line C-C of FIG. 5;|[0038] FIG. 7 is a sectional view taken along line B-B of FIG. 5;|[0039] FIG. 8 is a schematic view of the middle movable frame and the belt of the present invention;|[0040] FIG. 9 is a schematic illustration of a center belt of the present invention;|[0041] FIG. 10 is a partial schematic view of the middle annular soft plate and gear of the present invention;|[0042] FIG. 11 is a top view of a middle screen panel of the present invention;|[0043] in the figure: 1. moving the plate; 2. a movable frame; 3. a process cartridge; 4. rotating the rod; 5. a crushing knife; 6. a belt; 7. an annular soft plate; 8. a drive tooth; 9. an outlet hole; 10. a charging barrel; 11. a discharging barrel; 12. a stripper plate; 13. a baffle plate; 14. a first push rod; 15. a universal wheel; 16. a chute; 17. a slider; 18. a first motor; 19. a threaded rod; 20. a second motor; 21. a belt pulley; 22. a third motor; 23. an annular limiting groove; 24. a limiting block; 25. a fourth motor; 26. a first pneumatic telescopic rod; 27. a first spring; 28. a water tank is filled; 29. blocking; 30. blocking the rod; 31. a phase connecting rod; 32. a discharge hole; 33. a second pneumatic telescopic rod; 34. a fifth motor; 35. a connection plate; 36. a second push rod; 37. a second spring; 38. a striker plate; 39. a push block; 40. screening the plate; 41. fixing a cutting knife; 42. a movable plate; 43. moving the cutting knife; 44. a third spring; 45. a soil turning plate; 46. a gear; 47. fixing the rod; 48. and (5) fixing the bolt.|INVENTION MODE|Detailed Description|[0044] In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further described with the specific embodiments.|[0045] As shown in fig. 1 to 11, the carbon fixing device for increasing the waxberry artificial forest according to the present invention comprises a moving plate 1 symmetrically disposed;|[0046] the movable frame 2 is movably connected between the movable plates 1, a processing box 3 is fixedly connected to the inner side wall of the movable frame 2, a rotating rod 4 is connected to the inner side wall of the processing box 3 in a rotating mode, a crushing cutter 5 is fixedly connected to the rotating rod 4, two ends of the rotating rod 4 penetrate through the side wall of the processing box 3 and are fixedly connected with gears 46, an outlet hole 9 is formed in the lower end of the processing box 3, a belt 6 is connected to the inner side of the movable frame 2 in a transmission mode, the belt 6 is located on the outer side of the processing box 3, an annular soft plate 7 is fixedly connected to the upper portion of the belt 6, driving teeth 8 are fixedly connected to the side wall, opposite to the gears 46, of the annular soft plate 7, and the driving teeth 8 are meshed with the gears 46;|[0047] the lower part of the belt 6 is movably connected with a charging barrel 10, the bottom of the charging barrel 10 is movably connected with a discharging barrel 11, the inner side wall of the charging barrel 10 is symmetrically and obliquely and fixedly connected with a discharging plate 12, the discharging plate 12 is elastically connected with a baffle 13, and a first push rod 14 is connected between the baffle 13 and the discharging barrel 11.|[0048] The universal wheels 15 are installed at the bottom ends of the moving plates 1, and the moving plates 1 can move conveniently due to the arrangement of the universal wheels 15;|[0049] a sliding groove 16 is formed in the moving plate 1, a sliding block 17 is connected in the sliding groove 16 in a sliding manner, a first motor 18 is fixedly connected in the sliding groove 16, a threaded rod 19 is fixedly connected to a driving shaft of the first motor 18, the threaded rod 19 is in threaded connection with the sliding block 17, a second motor 20 is fixedly connected to the sliding block 17, a driving shaft of the second motor 20 is fixedly connected with the moving frame 2, the first motor 18 works to realize rotation of the threaded rod 19, the sliding block 17 moves in the rotating process of the threaded rod 19, and the position of the moving frame 2 is adjusted in the moving process of the sliding block 17; the second motor 20 operates to effect rotation of the movable frame 2, thereby adjusting the position of the movable frame 2.|[0050] The inside wall of activity frame 2 rotates and is connected with belt pulley 21, and 6 transmission connections of belt are between two belt pulleys 21, and fixedly connected with third motor 22 on the activity frame 2, third motor 22 and one of them belt pulley 21 fixed connection, and the belt pulley 21 rotation is realized in the work of third motor 22, because belt pulley 21 and belt 6 cooperate, consequently realize that belt 6 removes at belt pulley 21 pivoted in-process.|[0051] Seted up annular spacing groove 23 on the inside wall of adjustable frame 2, fixedly connected with stopper 24 on the lateral wall of belt 6, stopper 24 swing joint prevents that belt 6 from appearing the phenomenon of sinking at the in-process that removes in annular spacing groove 23 through annular spacing groove 23 and stopper 24's effect.|[0052] The lower end of the belt 6 is fixedly connected with a fourth motor 25, a driving shaft of the fourth motor 25 is fixedly connected with a first pneumatic telescopic rod 26, the movable end of the first pneumatic telescopic rod 26 is fixedly connected with the charging barrel 10, the fourth motor 25 works to realize the rotation of the charging barrel 10, the position of the charging barrel 10 is adjusted in the rotating process of the charging barrel 10, and the first pneumatic telescopic rod 26 works to realize the movement of the charging barrel 10 in the vertical direction, so that the movement of the charging barrel 10 in the vertical direction is adjusted;|[0053] fixedly connected with first spring 27 on stripper 12, the one end fixed connection of first spring 27 is on baffle 13, is convenient for realize through first spring 27 that baffle 13 elastic connection is on stripper 12.|[0054] A water charging box 28 is fixedly connected to the inner side wall of the charging barrel 10, water inlet holes are formed in the side walls of the water charging box 28 and the charging barrel 10, a blocking block 29 is connected to the water inlet hole in a threaded mode, water outlet holes are formed in the side walls of the water charging box 28 and the charging barrel 10, a blocking rod 30 is movably connected to the water outlet holes, the lower end of the blocking rod 30 is fixedly connected with a connecting rod 31, and the connecting rod 31 is fixedly connected with the discharging barrel 11;|[0055] the area value of the cross section of the phase connecting rod 31 is smaller than that of the cross section of the blocking rod 30, the blocking rod 30 moves upwards through the phase connecting rod 31 in the process that the discharging barrel 11 moves upwards, and water in the water containing tank 28 flows out through the water outlet hole conveniently because the area value of the cross section of the phase connecting rod 31 is smaller than that of the cross section of the blocking rod 30;|[0056] the lower end of the discharging barrel 11 is provided with a discharging hole 32.|[0057] The inner side wall of the charging barrel 10 is fixedly connected with a second pneumatic telescopic rod 33, the movable end of the second pneumatic telescopic rod 33 is fixedly connected with a fifth motor 34, the driving shaft of the fifth motor 34 is connected with an interconnection plate 35, a second push rod 36 is fixedly connected on the interconnection plate 35, the second pneumatic telescopic rod 33 works to realize the movement of the interconnection plate 35, the position of the link plate 35 is adjusted during the movement of the link plate 35, the fifth motor 34 is operated to rotate the link plate 35, the position of the connecting plate 35 is adjusted in the rotating process of the connecting plate 35, a third pneumatic telescopic rod is fixedly connected to a driving shaft of the fifth motor 34, the movable end of the third pneumatic telescopic rod is fixedly connected with the connecting plate 35, the third pneumatic telescopic rod and the second pneumatic telescopic rod 33 are vertically arranged, the third pneumatic telescopic rod works to realize that the connecting plate 35 moves in the horizontal direction, and the second pneumatic telescopic rod 33 works to realize that the connecting plate 35 moves in the vertical direction;|[0058] the accommodating groove is formed in the side wall of the outlet hole 9 of the processing box 3, the second spring 37 is fixedly connected in the accommodating groove, the striker plate 38 is fixedly connected on the second spring 37, the push block 39 is fixedly connected on the striker plate 38, the push block 39 corresponds to the second push rod 36, and when the second push rod 36 pushes the push block 39, the straw in the processing box 3 can fall out conveniently.|[0059] The screening plate 40 is fixedly connected to the inner side wall of the charging barrel 10, an outlet hole is formed in the screening plate 40, a fixed cutting knife 41 is fixedly connected to the side wall of the outlet hole, a movable plate 42 is movably connected to the inside of the outlet hole, a movable cutting knife 43 is fixedly connected to the movable plate 42, the movable cutting knife 43 is matched with the fixed cutting knife 41, the movable plate 42 corresponds to the second push rod 36, when straw exists on the screening plate 40, the second push rod 36 pushes the movable plate 42 to move the movable plate 42, the straw on the screening plate 40 is dropped between the fixed cutting knife 41 and the movable cutting knife 43 in the moving process of the movable plate 42, the movable cutting knife 43 is moved in the moving process of the movable plate 42, and the straw is cut due to the action of the movable cutting knife 43 and the fixed cutting knife 41;|[0060] the movable plate 42 is fixedly connected with a third spring 44, one end of the third spring 44 is fixedly connected to the side wall of the outlet hole, and the movable plate 42 is elastically connected in the outlet hole through the third spring 44.|[0061] The upper end of belt 6 is connected with dead lever 47 through fixing bolt 48, and fixedly connected with board 45 that digs on the dead lever 47 is convenient for realize the installation and the dismantlement of dead lever 47 on belt 6 through fixing bolt 48's setting, has realized the soil of digging to the waxberry woodland simultaneously because the effect of board 45 that digs.|[0062] A use method of a carbon sequestration device for improving a waxberry artificial forest comprises the following steps:|[0063] the third motor 22 works to realize the rotation of the belt pulley 21, and the belt pulley 21 is matched with the belt 6, so that the belt 6 moves in the rotation process of the belt pulley 21, and the movement of the annular soft plate 7 is realized, and the rotation of the rotating rod 4 in the processing box 3 is realized due to the driving teeth 8 arranged on the annular soft plate 7 and the matching of the driving teeth 8 and the gear 46, the rotation of the crushing knife 5 is realized in the rotation process of the rotating rod 4, and the chopping processing of the straws placed in the processing box 3 is realized in the rotation process of the crushing knife 5;|[0064] the fourth motor 25 works to realize the rotation of the charging barrel 10, the second push rod 36 moves in the rotation process of the charging barrel 10, when the second push rod 36 pushes the push block 39, the striker plate 38 moves through the push block 39, when one end of the striker plate 38 is not positioned in the outlet hole 9, the cut straws in the processing box 3 fall on the screening plate 40 from the outlet hole 9, the straws with smaller size fall below the screening plate 40 from a gap between the movable cutting knife 43 and the fixed cutting knife 41, the straws with larger size are positioned on the screening plate 40, the second pneumatic telescopic rod 33 works to realize the downward movement of the connecting plate 35, then the fifth motor 34 works to realize the rotation of the connecting plate 35, so that the second push rod 36 is positioned on the upper surface of the screening plate 40, the third pneumatic telescopic rod works to realize the horizontal movement of the second push rod 36, when the second push rod 36 moves horizontally, the movable plate 42 moves, the straws on the screening plate 40 fall between the fixed cutting knife 41 and the movable cutting knife 43 in the moving process of the movable plate 42, and the movable cutting knife 43 moves in the moving process of the movable plate 42, so that the straws are cut under the action of the movable cutting knife 43 and the fixed cutting knife 41;|[0065] a worker visually observes whether straws exist on the ground of the waxberry forest land or not, and if the straws do not exist or the quantity of the straws is less, the worker visually observes that whether the straws exist on the ground of the waxberry forest land or not. The charging barrel 10 moves downwards when the first pneumatic telescopic rod 26 works, the charging barrel 11 moves downwards in the downward movement process of the charging barrel 10, when the bottom of the charging barrel 11 is in contact with the ground of a waxberry forest land, the charging barrel 11 moves upwards, the baffle 13 moves through the first push rod 14 when the charging barrel 11 moves upwards, straw located on the discharging plate 12 drops in the charging barrel 11 conveniently, and then the straw drops on the ground of the waxberry forest land through the discharging hole 32 of the charging barrel 11.|[0066] The working principle is as follows: the staff places the straw in processing box 3, third motor 22 work realizes that belt pulley 21 rotates, because belt pulley 21 cooperatees with belt 6, consequently realize belt 6 and remove at belt pulley 21 pivoted in-process, thereby realize that annular soft board 7 removes, because be provided with drive tooth 8 on the annular soft board 7, because drive tooth 8 cooperatees with gear 46, thereby realize dwang 4 at the internal rotation of processing box 3, realize broken sword 5 at dwang 4 pivoted in-process and rotate, realize the shredding process to placing the straw in processing box 3 at broken sword 5 pivoted in-process.|[0067] The fourth motor 25 works to realize the rotation of the charging barrel 10, the second push rod 36 moves in the rotation process of the charging barrel 10, when the second push rod 36 pushes the push block 39, the striker plate 38 moves through the push block 39, when one end of the striker plate 38 is not positioned in the outlet hole 9, the cut straws in the processing box 3 fall on the screening plate 40 from the outlet hole 9, the straws with smaller size fall below the screening plate 40 from a gap between the movable cutting knife 43 and the fixed cutting knife 41, the straws with larger size are positioned on the screening plate 40, the second pneumatic telescopic rod 33 works to realize the downward movement of the connecting plate 35, then the fifth motor 34 works to realize the rotation of the connecting plate 35, so that the second push rod 36 is positioned on the upper surface of the screening plate 40, the third pneumatic telescopic rod works to realize the horizontal movement of the second push rod 36, when the second push rod 36 moves horizontally, the movable plate 42 moves, the straw on the screening plate 40 falls between the fixed cutting knife 41 and the movable cutting knife 43 in the moving process of the movable plate 42, and the movable cutting knife 43 moves in the moving process of the movable plate 42, so that the straw is cut under the action of the movable cutting knife 43 and the fixed cutting knife 41.|[0068] The charging barrel 10 moves downwards when the first pneumatic telescopic rod 26 works, the charging barrel 11 moves downwards in the downward movement process of the charging barrel 10, when the bottom of the charging barrel 11 is in contact with the ground of a waxberry forest land, the charging barrel 11 moves upwards, the baffle 13 moves through the first push rod 14 when the charging barrel 11 moves upwards, straw located on the discharging plate 12 drops in the charging barrel 11 conveniently, and then the straw drops on the ground of the waxberry forest land through the discharging hole 32 of the charging barrel 11.|[0069] In the process that the discharging barrel 11 moves upwards, the blocking rod 30 moves upwards through the phase connecting rod 31, and the area value of the cross section of the phase connecting rod 31 is smaller than that of the cross section of the blocking rod 30, so that water in the water containing tank 28 can flow out through the water outlet holes, and watering treatment of the waxberry forest land is achieved.|[0070] When covering the straw on the waxberry woodland, dig out the sunken hole ground on the ground of waxberry woodland manually, second motor 20 work realizes that movable frame 2 rotates, until turning over native board 45 and being located the below of movable frame 2, and make turning over native board 45 be located sunken hole internal, third motor 22 work realizes realizing belt pulley 21 and rotates, because belt pulley 21 cooperatees with belt 6, consequently realize belt 6 and remove at belt pulley 21 pivoted in-process, realize turning over native board 45 and remove when belt 6 removes, realize turning over the soil to the soil that covers there is the straw when turning over native board 45 and remove and handle, be convenient for make the straw be located the soil sack.|[0071] The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and the embodiments and descriptions given above are only illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which fall within the scope of the claims. The scope of the invention is defined by the appended claims and equivalents thereof. (CN113396708)|TECHNICAL FIELD|[0001] The invention relates to the technical field of carbon sequestration of artificial forests, in particular to a carbon sequestration device for improving a waxberry artificial forest and a using method thereof.|BACKGROUND ART|[0002] The waxberry is an important fruit tree in subtropical zones in China, the planting area reaches 150 million hectares, the fruit has unique flavor and high nutritive value, and the waxberry is popular among people. However, due to excessive management, the shrub layer and the herbaceous layer under the tree are completely disappeared, water and soil loss is serious, the carbon fixing capacity of the vegetable layer under the waxberry tree is obviously reduced, organic carbon in the soil is lost, and the carbon fixing capacity of the artificial waxberry forest and the exertion of other forest functions are seriously damaged. Therefore, the key technology for improving the carbon fixing capacity of the waxberry artificial forest has very important significance for providing technical storage for responding to global carbon trading and improving the carbon fixing capacity of the waxberry artificial forest to the maximum extent.|[0003] However, in the existing carbon sequestration method for the artificial red bayberry forest, before the straws are laid on the ground of the red bayberry forest land, in order to better improve the biomass carbon and the soil organic carbon storage amount, the straws need to be shredded by additional shredding equipment and then laid on the red bayberry forest land by conveying equipment, and this method needs to be operated by a worker in advance, prolongs the treatment time, and when the straws are shredded by additional shredding equipment in other places, the straws are easy to splash after being shredded, thereby causing the waste of straw raw materials.|DISCLOSURE|Disclosure of Invention|[0004] Aiming at the problems in the prior art, the invention provides a carbon fixation device for improving a waxberry artificial forest and a using method thereof.|[0005] The technical scheme adopted by the invention for solving the technical problems is as follows: a carbon fixation device for improving the waxberry artificial forest comprises symmetrically arranged moving plates;|[0006] the movable frame is movably connected between the movable plates, a processing box is fixedly connected to the inner side wall of the movable frame, a rotating rod is connected to the inner rotation of the processing box, a crushing cutter is fixedly connected to the rotating rod, two ends of the rotating rod penetrate through the side wall of the processing box and are fixedly connected with gears, an outlet hole is formed in the lower end of the processing box, a belt is connected to the movable frame in a transmission mode and is located on the outer side of the processing box, an annular soft plate is fixedly connected to the upper portion of the belt, driving teeth are fixedly connected to the side wall of the annular soft plate, opposite to the gears, and the driving teeth are meshed with the gears;|[0007] the feeding device is characterized in that a charging barrel is movably connected below the belt, a discharging barrel is movably connected at the bottom of the charging barrel, discharging plates are symmetrically, obliquely and fixedly connected to the inner side wall of the charging barrel, a baffle is elastically connected to the discharging plates, and a first push rod is connected between the baffle and the discharging barrel.|[0008] The bottom end of the moving plate is provided with a universal wheel;|[0009] the movable plate is provided with a sliding groove, a sliding block is connected in the sliding groove in a sliding mode, a first motor is fixedly connected in the sliding groove, a threaded rod is fixedly connected to the driving shaft of the first motor, the threaded rod is in threaded connection with the sliding block, a second motor is fixedly connected to the sliding block, and the driving shaft of the second motor is fixedly connected with the movable frame.|[0010] The inside wall of activity frame rotates and is connected with the belt pulley, belt transmission connects between two belt pulleys, fixedly connected with third motor on the activity frame, third motor and one of them belt pulley fixed connection.|[0011] An annular limiting groove is formed in the inner side wall of the movable frame, a limiting block is fixedly connected to the outer side wall of the belt, and the limiting block is movably connected to the annular limiting groove.|[0012] The lower end of the belt is fixedly connected with a fourth motor, a driving shaft of the fourth motor is fixedly connected with a first pneumatic telescopic rod, and the movable end of the first pneumatic telescopic rod is fixedly connected with the charging barrel;|[0013] the stripper plate is fixedly connected with a first spring, and one end of the first spring is fixedly connected to the baffle plate.|[0014] The inner side wall of the charging barrel is fixedly connected with a water charging tank, the side walls of the water charging tank and the charging barrel are both provided with water inlet holes, the water inlet holes are in threaded connection with a blocking block, the side walls of the water charging tank and the charging barrel are both provided with water outlet holes, blocking rods are movably connected in the water outlet holes, the lower ends of the blocking rods are fixedly connected with phase connecting rods, and the phase connecting rods are fixedly connected with the discharging barrel;|[0015] the area value of the cross section of the phase connecting rod is smaller than that of the cross section of the blocking rod;|[0016] the lower end of the discharge barrel is provided with a discharge hole.|[0017] A second pneumatic telescopic rod is fixedly connected to the inner side wall of the charging barrel, a fifth motor is fixedly connected to the movable end of the second pneumatic telescopic rod, a driving shaft of the fifth motor is connected with a connecting plate, and a second push rod is fixedly connected to the connecting plate;|[0018] the accommodating groove is formed in the outlet side wall of the processing box, a second spring is fixedly connected in the accommodating groove, a material baffle plate is fixedly connected to the second spring, a pushing block is fixedly connected to the material baffle plate, and the pushing block corresponds to the second push rod.|[0019] A screening plate is fixedly connected to the inner side wall of the charging barrel, an outlet hole is formed in the screening plate, a fixed cutting knife is fixedly connected to the side wall of the outlet hole, a movable plate is movably connected to the outlet hole, a movable cutting knife is fixedly connected to the movable plate, the movable cutting knife is matched with the fixed cutting knife, and the movable plate corresponds to the second push rod;|[0020] the movable plate is fixedly connected with a third spring, and one end of the third spring is fixedly connected to the side wall of the outlet hole.|[0021] The upper end of the belt is connected with a fixed rod through a fixed bolt, and the fixed rod is fixedly connected with a soil turning plate.|[0022] A use method of a carbon sequestration device for improving a waxberry artificial forest comprises the following steps:|[0023] the third motor works to realize the rotation of the belt pulley, and the belt pulley is matched with the belt, so that the belt is moved in the rotation process of the belt pulley, and the movement of the annular soft plate is realized;|[0024] the fourth motor works to realize the rotation of the charging barrel, the second push rod moves in the rotating process of the charging barrel, when the second push rod pushes the push block, the baffle plate moves through the push block, when one end of the baffle plate is not positioned in the outlet hole, the cut straws in the processing box fall on the screening plate from the outlet hole, the straws with smaller size fall to the lower part of the screening plate from a gap between the movable cutting knife and the fixed cutting knife, the straws with larger size are positioned on the screening plate, the second pneumatic telescopic rod works to realize the downward movement of the connecting plate, then the fifth motor works to realize the rotation of the connecting plate, so that the second push rod is positioned on the upper surface of the screening plate, the third pneumatic telescopic rod works to realize the movement of the second push rod in the horizontal direction, when the second push rod moves in the horizontal direction, the movable plate moves, the straws on the screening plate fall between the fixed cutting knife and the movable cutting knife in the moving process of the movable plate, meanwhile, the movable cutting knife is moved in the moving process of the movable plate, and the movable cutting knife and the fixed cutting knife are used for cutting straws;|[0025] the charging barrel moves downwards when the first pneumatic telescopic rod works, the charging barrel moves downwards in the process of moving downwards of the charging barrel, when the bottom of the discharging barrel is in contact with the ground of a waxberry forest land, the discharging barrel moves upwards, the baffle moves through the first push rod when the discharging barrel moves upwards, straw on the discharging plate drops in the discharging barrel conveniently, and then the straw drops on the ground of the waxberry forest land through the discharging hole of the discharging barrel.|[0026] The invention has the beneficial effects that:|[0027] through setting up the section of thick bamboo of charging in the below of belt, the straw after will handling a section of thick bamboo breakage drops in the section of thick bamboo of charging, the belt pulley rotation is realized in third motor work, because the belt pulley cooperatees with the belt, consequently, it removes to realize the belt at belt pulley pivoted in-process, the in-process that removes at the belt realizes the section of thick bamboo of charging and removes, thereby be convenient for be equipped with the straw in the section of thick bamboo of charging and cover subaerial at the bayberry forest land, this layer biomass carbon of bayberry forest grass and soil organic carbon storage have been improved, the quality of bayberry fruit has also obviously been improved simultaneously, the carbon fixation ability of bayberry forest vegetable layer obviously improves, effectively prevent soil organic carbon loss.|[0028] Through setting up the dwang in the processing box to be provided with broken sword on the dwang, because drive tooth and gear on the annular soft board cooperate, consequently realize gear revolve through the annular soft board when the belt removes, realize the dwang at gear revolve's in-process and rotate, thereby realize the processing of cutting up of straw to being located the processing box.|[0029] The water tank is arranged in the charging barrel, so that the waxberry forest land is watered conveniently. In the process of upward movement of the discharge barrel, the upward movement of the blocking rod is realized through the connecting rod, and the area value of the cross section of the connecting rod is smaller than that of the cross section of the blocking rod, so that water in the water containing tank flows out through the water outlet hole, and the watering treatment of the waxberry forest land is realized.|[0030] The method improves the biomass carbon of the herbaceous layer of the waxberry forest and the organic carbon storage amount of the soil, obviously improves the quality of waxberry fruits, obviously improves the carbon fixation capacity of the vegetable layer of the waxberry forest, and effectively prevents the organic carbon loss of the soil.|DRAWINGS DESCRIPTION|[0031] The invention is further illustrated with reference to the following figures and examples.|[0032] FIG. 1 is a schematic view of the present invention;|[0033] FIG. 2 is an enlarged view of a portion of FIG. 1 at A;|[0034] FIG. 3 is a schematic view of the interior of the charging barrel and the discharging barrel of the present invention;|[0035] FIG. 4 is an enlarged view of a portion of FIG. 3 at B;|[0036] FIG. 5 is a schematic view of a middle process cartridge according to the present invention;|[0037] FIG. 6 is a cross-sectional view taken along line C-C of FIG. 5;|[0038] FIG. 7 is a sectional view taken along line B-B of FIG. 5;|[0039] FIG. 8 is a schematic view of the middle movable frame and the belt of the present invention;|[0040] FIG. 9 is a schematic illustration of a center belt of the present invention;|[0041] FIG. 10 is a partial schematic view of the middle annular soft plate and gear of the present invention;|[0042] FIG. 11 is a top view of a middle screen panel of the present invention;|[0043] in the figure: 1. moving the plate; 2. a movable frame; 3. a process cartridge; 4. rotating the rod; 5. a crushing knife; 6. a belt; 7. an annular soft plate; 8. a drive tooth; 9. an outlet hole; 10. a charging barrel; 11. a discharging barrel; 12. a stripper plate; 13. a baffle plate; 14. a first push rod; 15. a universal wheel; 16. a chute; 17. a slider; 18. a first motor; 19. a threaded rod; 20. a second motor; 21. a belt pulley; 22. a third motor; 23. an annular limiting groove; 24. a limiting block; 25. a fourth motor; 26. a first pneumatic telescopic rod; 27. a first spring; 28. a water tank is filled; 29. blocking; 30. blocking the rod; 31. a phase connecting rod; 32. a discharge hole; 33. a second pneumatic telescopic rod; 34. a fifth motor; 35. a connection plate; 36. a second push rod; 37. a second spring; 38. a striker plate; 39. a push block; 40. screening the plate; 41. fixing a cutting knife; 42. a movable plate; 43. moving the cutting knife; 44. a third spring; 45. a soil turning plate; 46. a gear; 47. fixing the rod; 48. and (5) fixing the bolt.|INVENTION MODE|Detailed Description|[0044] In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further described with the specific embodiments.|[0045] As shown in fig. 1 to 11, the carbon fixing device for increasing the waxberry artificial forest according to the present invention comprises a moving plate 1 symmetrically disposed;|[0046] the movable frame 2 is movably connected between the movable plates 1, a processing box 3 is fixedly connected to the inner side wall of the movable frame 2, a rotating rod 4 is connected to the inner side wall of the processing box 3 in a rotating mode, a crushing cutter 5 is fixedly connected to the rotating rod 4, two ends of the rotating rod 4 penetrate through the side wall of the processing box 3 and are fixedly connected with gears 46, an outlet hole 9 is formed in the lower end of the processing box 3, a belt 6 is connected to the inner side of the movable frame 2 in a transmission mode, the belt 6 is located on the outer side of the processing box 3, an annular soft plate 7 is fixedly connected to the upper portion of the belt 6, driving teeth 8 are fixedly connected to the side wall, opposite to the gears 46, of the annular soft plate 7, and the driving teeth 8 are meshed with the gears 46;|[0047] the lower part of the belt 6 is movably connected with a charging barrel 10, the bottom of the charging barrel 10 is movably connected with a discharging barrel 11, the inner side wall of the charging barrel 10 is symmetrically and obliquely and fixedly connected with a discharging plate 12, the discharging plate 12 is elastically connected with a baffle 13, and a first push rod 14 is connected between the baffle 13 and the discharging barrel 11.|[0048] The universal wheels 15 are installed at the bottom ends of the moving plates 1, and the moving plates 1 can move conveniently due to the arrangement of the universal wheels 15;|[0049] a sliding groove 16 is formed in the moving plate 1, a sliding block 17 is connected in the sliding groove 16 in a sliding manner, a first motor 18 is fixedly connected in the sliding groove 16, a threaded rod 19 is fixedly connected to a driving shaft of the first motor 18, the threaded rod 19 is in threaded connection with the sliding block 17, a second motor 20 is fixedly connected to the sliding block 17, a driving shaft of the second motor 20 is fixedly connected with the moving frame 2, the first motor 18 works to realize rotation of the threaded rod 19, the sliding block 17 moves in the rotating process of the threaded rod 19, and the position of the moving frame 2 is adjusted in the moving process of the sliding block 17; the second motor 20 operates to effect rotation of the movable frame 2, thereby adjusting the position of the movable frame 2.|[0050] The inside wall of activity frame 2 rotates and is connected with belt pulley 21, and 6 transmission connections of belt are between two belt pulleys 21, and fixedly connected with third motor 22 on the activity frame 2, third motor 22 and one of them belt pulley 21 fixed connection, and the belt pulley 21 rotation is realized in the work of third motor 22, because belt pulley 21 and belt 6 cooperate, consequently realize that belt 6 removes at belt pulley 21 pivoted in-process.|[0051] Seted up annular spacing groove 23 on the inside wall of adjustable frame 2, fixedly connected with stopper 24 on the lateral wall of belt 6, stopper 24 swing joint prevents that belt 6 from appearing the phenomenon of sinking at the in-process that removes in annular spacing groove 23 through annular spacing groove 23 and stopper 24's effect.|[0052] The lower end of the belt 6 is fixedly connected with a fourth motor 25, a driving shaft of the fourth motor 25 is fixedly connected with a first pneumatic telescopic rod 26, the movable end of the first pneumatic telescopic rod 26 is fixedly connected with the charging barrel 10, the fourth motor 25 works to realize the rotation of the charging barrel 10, the position of the charging barrel 10 is adjusted in the rotating process of the charging barrel 10, and the first pneumatic telescopic rod 26 works to realize the movement of the charging barrel 10 in the vertical direction, so that the movement of the charging barrel 10 in the vertical direction is adjusted;|[0053] fixedly connected with first spring 27 on stripper 12, the one end fixed connection of first spring 27 is on baffle 13, is convenient for realize through first spring 27 that baffle 13 elastic connection is on stripper 12.|[0054] A water charging box 28 is fixedly connected to the inner side wall of the charging barrel 10, water inlet holes are formed in the side walls of the water charging box 28 and the charging barrel 10, a blocking block 29 is connected to the water inlet hole in a threaded mode, water outlet holes are formed in the side walls of the water charging box 28 and the charging barrel 10, a blocking rod 30 is movably connected to the water outlet holes, the lower end of the blocking rod 30 is fixedly connected with a connecting rod 31, and the connecting rod 31 is fixedly connected with the discharging barrel 11;|[0055] the area value of the cross section of the phase connecting rod 31 is smaller than that of the cross section of the blocking rod 30, the blocking rod 30 moves upwards through the phase connecting rod 31 in the process that the discharging barrel 11 moves upwards, and water in the water containing tank 28 flows out through the water outlet hole conveniently because the area value of the cross section of the phase connecting rod 31 is smaller than that of the cross section of the blocking rod 30;|[0056] the lower end of the discharging barrel 11 is provided with a discharging hole 32.|[0057] The inner side wall of the charging barrel 10 is fixedly connected with a second pneumatic telescopic rod 33, the movable end of the second pneumatic telescopic rod 33 is fixedly connected with a fifth motor 34, the driving shaft of the fifth motor 34 is connected with an interconnection plate 35, a second push rod 36 is fixedly connected on the interconnection plate 35, the second pneumatic telescopic rod 33 works to realize the movement of the interconnection plate 35, the position of the link plate 35 is adjusted during the movement of the link plate 35, the fifth motor 34 is operated to rotate the link plate 35, the position of the connecting plate 35 is adjusted in the rotating process of the connecting plate 35, a third pneumatic telescopic rod is fixedly connected to a driving shaft of the fifth motor 34, the movable end of the third pneumatic telescopic rod is fixedly connected with the connecting plate 35, the third pneumatic telescopic rod and the second pneumatic telescopic rod 33 are vertically arranged, the third pneumatic telescopic rod works to realize that the connecting plate 35 moves in the horizontal direction, and the second pneumatic telescopic rod 33 works to realize that the connecting plate 35 moves in the vertical direction;|[0058] the accommodating groove is formed in the side wall of the outlet hole 9 of the processing box 3, the second spring 37 is fixedly connected in the accommodating groove, the striker plate 38 is fixedly connected on the second spring 37, the push block 39 is fixedly connected on the striker plate 38, the push block 39 corresponds to the second push rod 36, and when the second push rod 36 pushes the push block 39, the straw in the processing box 3 can fall out conveniently.|[0059] The screening plate 40 is fixedly connected to the inner side wall of the charging barrel 10, an outlet hole is formed in the screening plate 40, a fixed cutting knife 41 is fixedly connected to the side wall of the outlet hole, a movable plate 42 is movably connected to the inside of the outlet hole, a movable cutting knife 43 is fixedly connected to the movable plate 42, the movable cutting knife 43 is matched with the fixed cutting knife 41, the movable plate 42 corresponds to the second push rod 36, when straw exists on the screening plate 40, the second push rod 36 pushes the movable plate 42 to move the movable plate 42, the straw on the screening plate 40 is dropped between the fixed cutting knife 41 and the movable cutting knife 43 in the moving process of the movable plate 42, the movable cutting knife 43 is moved in the moving process of the movable plate 42, and the straw is cut due to the action of the movable cutting knife 43 and the fixed cutting knife 41;|[0060] the movable plate 42 is fixedly connected with a third spring 44, one end of the third spring 44 is fixedly connected to the side wall of the outlet hole, and the movable plate 42 is elastically connected in the outlet hole through the third spring 44.|[0061] The upper end of belt 6 is connected with dead lever 47 through fixing bolt 48, and fixedly connected with board 45 that digs on the dead lever 47 is convenient for realize the installation and the dismantlement of dead lever 47 on belt 6 through fixing bolt 48's setting, has realized the soil of digging to the waxberry woodland simultaneously because the effect of board 45 that digs.|[0062] A use method of a carbon sequestration device for improving a waxberry artificial forest comprises the following steps:|[0063] the third motor 22 works to realize the rotation of the belt pulley 21, and the belt pulley 21 is matched with the belt 6, so that the belt 6 moves in the rotation process of the belt pulley 21, and the movement of the annular soft plate 7 is realized, and the rotation of the rotating rod 4 in the processing box 3 is realized due to the driving teeth 8 arranged on the annular soft plate 7 and the matching of the driving teeth 8 and the gear 46, the rotation of the crushing knife 5 is realized in the rotation process of the rotating rod 4, and the chopping processing of the straws placed in the processing box 3 is realized in the rotation process of the crushing knife 5;|[0064] the fourth motor 25 works to realize the rotation of the charging barrel 10, the second push rod 36 moves in the rotation process of the charging barrel 10, when the second push rod 36 pushes the push block 39, the striker plate 38 moves through the push block 39, when one end of the striker plate 38 is not positioned in the outlet hole 9, the cut straws in the processing box 3 fall on the screening plate 40 from the outlet hole 9, the straws with smaller size fall below the screening plate 40 from a gap between the movable cutting knife 43 and the fixed cutting knife 41, the straws with larger size are positioned on the screening plate 40, the second pneumatic telescopic rod 33 works to realize the downward movement of the connecting plate 35, then the fifth motor 34 works to realize the rotation of the connecting plate 35, so that the second push rod 36 is positioned on the upper surface of the screening plate 40, the third pneumatic telescopic rod works to realize the horizontal movement of the second push rod 36, when the second push rod 36 moves horizontally, the movable plate 42 moves, the straws on the screening plate 40 fall between the fixed cutting knife 41 and the movable cutting knife 43 in the moving process of the movable plate 42, and the movable cutting knife 43 moves in the moving process of the movable plate 42, so that the straws are cut under the action of the movable cutting knife 43 and the fixed cutting knife 41;|[0065] a worker visually observes whether straws exist on the ground of the waxberry forest land or not, and if the straws do not exist or the quantity of the straws is less, the worker visually observes that whether the straws exist on the ground of the waxberry forest land or not. The charging barrel 10 moves downwards when the first pneumatic telescopic rod 26 works, the charging barrel 11 moves downwards in the downward movement process of the charging barrel 10, when the bottom of the charging barrel 11 is in contact with the ground of a waxberry forest land, the charging barrel 11 moves upwards, the baffle 13 moves through the first push rod 14 when the charging barrel 11 moves upwards, straw located on the discharging plate 12 drops in the charging barrel 11 conveniently, and then the straw drops on the ground of the waxberry forest land through the discharging hole 32 of the charging barrel 11.|[0066] The working principle is as follows: the staff places the straw in processing box 3, third motor 22 work realizes that belt pulley 21 rotates, because belt pulley 21 cooperatees with belt 6, consequently realize belt 6 and remove at belt pulley 21 pivoted in-process, thereby realize that annular soft board 7 removes, because be provided with drive tooth 8 on the annular soft board 7, because drive tooth 8 cooperatees with gear 46, thereby realize dwang 4 at the internal rotation of processing box 3, realize broken sword 5 at dwang 4 pivoted in-process and rotate, realize the shredding process to placing the straw in processing box 3 at broken sword 5 pivoted in-process.|[0067] The fourth motor 25 works to realize the rotation of the charging barrel 10, the second push rod 36 moves in the rotation process of the charging barrel 10, when the second push rod 36 pushes the push block 39, the striker plate 38 moves through the push block 39, when one end of the striker plate 38 is not positioned in the outlet hole 9, the cut straws in the processing box 3 fall on the screening plate 40 from the outlet hole 9, the straws with smaller size fall below the screening plate 40 from a gap between the movable cutting knife 43 and the fixed cutting knife 41, the straws with larger size are positioned on the screening plate 40, the second pneumatic telescopic rod 33 works to realize the downward movement of the connecting plate 35, then the fifth motor 34 works to realize the rotation of the connecting plate 35, so that the second push rod 36 is positioned on the upper surface of the screening plate 40, the third pneumatic telescopic rod works to realize the horizontal movement of the second push rod 36, when the second push rod 36 moves horizontally, the movable plate 42 moves, the straw on the screening plate 40 falls between the fixed cutting knife 41 and the movable cutting knife 43 in the moving process of the movable plate 42, and the movable cutting knife 43 moves in the moving process of the movable plate 42, so that the straw is cut under the action of the movable cutting knife 43 and the fixed cutting knife 41.|[0068] The charging barrel 10 moves downwards when the first pneumatic telescopic rod 26 works, the charging barrel 11 moves downwards in the downward movement process of the charging barrel 10, when the bottom of the charging barrel 11 is in contact with the ground of a waxberry forest land, the charging barrel 11 moves upwards, the baffle 13 moves through the first push rod 14 when the charging barrel 11 moves upwards, straw located on the discharging plate 12 drops in the charging barrel 11 conveniently, and then the straw drops on the ground of the waxberry forest land through the discharging hole 32 of the charging barrel 11.|[0069] In the process that the discharging barrel 11 moves upwards, the blocking rod 30 moves upwards through the phase connecting rod 31, and the area value of the cross section of the phase connecting rod 31 is smaller than that of the cross section of the blocking rod 30, so that water in the water containing tank 28 can flow out through the water outlet holes, and watering treatment of the waxberry forest land is achieved.|[0070] When covering the straw on the waxberry woodland, dig out the sunken hole ground on the ground of waxberry woodland manually, second motor 20 work realizes that movable frame 2 rotates, until turning over native board 45 and being located the below of movable frame 2, and make turning over native board 45 be located sunken hole internal, third motor 22 work realizes realizing belt pulley 21 and rotates, because belt pulley 21 cooperatees with belt 6, consequently realize belt 6 and remove at belt pulley 21 pivoted in-process, realize turning over native board 45 and remove when belt 6 removes, realize turning over the soil to the soil that covers there is the straw when turning over native board 45 and remove and handle, be convenient for make the straw be located the soil sack.|[0071] The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and the embodiments and descriptions given above are only illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which fall within the scope of the claims. The scope of the invention is defined by the appended claims and equivalents thereof. Family Number|(96148517)|96148517|Abstract|(CN113396708 A)|The invention relates to the technical field of carbon sequestration of artificial forests , in particular to a carbon sequestration device for improving a waxberry artificial forest and a use method of the carbon sequestration device . The carbon sequestration device comprises movable plates which are symmetrically arranged ; a movable frame is movably connected between the movable plates , a processing box is fixedly connected to the inner side wall of the movable frame , a rotating rod is rotationally connected to the interior of the processing box , a crushing cutter is fixedly connected to the rotating rod , the two ends of the rotating rod penetrate through the side wall of the processing box and are fixedly connected with gears , an outlet hole is formed in the lower end of the processing box , and a belt is in transmission connection with the interior of the movable frame and is located on the outer side of the processing box . According to the carbon sequestration device , the biomass carbon and soil organic carbon storage amount of a waxberry forest herbaceous layer is increased , meanwhile , the quality of waxberry fruits is obviously improved , the carbon sequestration capacity of a waxberry forest vegetation layer is obviously improved , and soil organic carbon loss is effectively prevented . |CPC codes|(CN113396708 A)|A01F - 029/08 |A01F - 029/09/5 |A01F - 029/09 |IPC codes|(CN113396708 A)|A01F - 029/08 |A01F - 029/09 |Title|(CN113396708 A)|Carbon sequestration device for improving waxberry artificial forest and use method of carbon sequestration device | Other special machines A01F-029/08|A01F-029/09|A01F-029/09/5 A01F-029/08|A01F-029/09|A01F-029/09/5 A01F-029/08|A01F-029/09 A01F-029/08|A01F-029/09 CN111615939|CN209002404U|CN108811807|CN207401561U|CN106332611|JP2011177148|BE-898715 CN111615939 90500677 WHO=Examiner SELF=N CAT=A|CN209002404U 84962274 WHO=Examiner SELF=N CAT=A|CN108811807 82022330 WHO=Examiner SELF=N CAT=A|CN207401561U 79859996 WHO=Examiner SELF=N CAT=A|CN106332611 75187287 WHO=Examiner SELF=N CAT=A|JP2011177148 7927135 WHO=Examiner SELF=N CAT=A|BE-898715 2365636 WHO=Examiner SELF=N CAT=A BE-898715; JP2011177148; CN106332611; CN207401561U; CN108811807; CN209002404U; CN111615939 LAPSED (CN113396708)|LAPSED DEAD (CN113396708)|DEAD (CN113396708)|LEGAL DETAILS FOR CN113396708|Actual or expected expiration date=2022-12-16|Legal state=DEAD|Status=LAPSED|Event publication date=2021-06-17|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202110672589|Application date=2021-06-17|Standardized application number=2021CN-0672589|Event publication date=2021-09-17|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN113396708|Publication stage code=A|Publication date=2021-09-17|Standardized publication number=CN113396708|Event publication date=2021-09-17|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2021-10-08|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2022-12-16|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRi9B1n8QfZdFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000059030506&ekey=2196&xpn=CN113396708&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=gQQx0VNGSiHlOBoA4vHdpZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN113396708)|CN (CN113396708)|NAME=ZHEJIANG A&F UNIVERSITY , COUNTRY=CN (CN113396708)|NAME=PAN FANGHUA;ANHUA MEI SHAN PATENT BUSINESS OFFICE, ANHUA COUNTY , REG=43005 (CN113396708)|NAME=ZHANG YONG|NAME=WANG ZENG|NAME=PENG XINYI|NAME=YANG SHUNING|NAME=CAI YANJIANG|NAME=WU JIASEN|NAME=HUANG YUJIE|NAME=WANG JIANWU|NAME=YE LIMIN 0 1 Titre: (CN113396708)|Carbon sequestration device for improving waxberry artificial forest and use method of carbon sequestration device Résumé: (CN113396708)|The invention relates to the technical field of carbon sequestration of artificial forests, in particular to a carbon sequestration device for improving a waxberry artificial forest and a use method of the carbon sequestration device. The carbon sequestration device comprises movable plates which are symmetrically arranged; a movable frame is movably connected between the movable plates, a processing box is fixedly connected to the inner side wall of the movable frame, a rotating rod is rotationally connected to the interior of the processing box, a crushing cutter is fixedly connected to the rotating rod, the two ends of the rotating rod penetrate through the side wall of the processing box and are fixedly connected with gears, an outlet hole is formed in the lower end of the processing box, and a belt is in transmission connection with the interior of the movable frame and is located on the outer side of the processing box. According to the carbon sequestration device, the biomass carbon and soil organic carbon storage amount of a waxberry forest herbaceous layer is increased, meanwhile, the quality of waxberry fruits is obviously improved, the carbon sequestration capacity of a waxberry forest vegetation layer is obviously improved, and soil organic carbon loss is effectively prevented. 21 Abstract gpt-4o-mini no The article focuses on a carbon sequestration device for improving biomass and soil organic carbon in a specific forest type, without addressing mineral weathering or CO₂ capture through mineral processes.
23 CN202211562265 CN202211562265 CN115843544 104310198 CN115843544 A 2023-03-28 [CN115843544] 2022-12-07 2022-12-07 2023-03-28 (CN115843544)|2023-09-22 (CN115843544)|Application structure and method for improving soil carbon sequestration effect of straw crushing, mixing and returning (CN115843544)|The invention provides an application structure and method for improving the soil carbon sequestration effect of straw crushing, mixing and returning. The application structure comprises a moving trolley, a rack, a cutter assembly, a driving structure and a decomposition agent adding assembly. The driving structure is connected with the material scattering roller to drive the material scattering roller to rotate, and materials in the material scattering roller evenly and slowly flow out of the small material scattering holes. When straw is cut, decomposition agent materials are put into the material scattering roller through the material adding barrel, and the material scattering roller can slowly and uniformly scatter the materials into the straw through the rotation effect, so that the purposes of cutting, crushing and field changing of the straw and adding of the decomposition agent materials can be achieved at the same time; the working process is simplified, the carbon sequestration effect of straw returning is improved, and the good application effect is achieved. HEILONGJIANG AGRICULTURAL ECONOMY VOCATIONAL COLLEGE (CN115843544)|HEILONGJIANG AGRICULTURAL ECONOMY VOCATIONAL College ([CN]) TONG SHUYUAN|DU ZHENYU|LIANG XUANHE|XU WENDONG|WANG HAILONG|SUN PINGPING|XU JIFA|WANG ZEJIA|WANG TIANYE|WANG XING|WANG XIANRUI (CN115843544)|TONG SHUYUAN|DU ZHENYU|LIANG XUANHE|XU WENDONG|WANG HAILONG|SUN PINGPING|XU JIFA|WANG ZEJIA|WANG TIANYE|WANG XING|WANG XIANRUI (CN115843544)|LIU LIJUAN;Shenyang Yinuojunke Intellectual Property Agency (General Partnership)|Reg. Nb: 21266 (CN115843544)|The hard tube section is inserted into the spreader roller when it is desired to feed, the closure plate is opened when it is not desired to remove the hard tube section when feeding is desired, and the closure plate is closed and the spreader roller is rotated to spread the material.| (CN115843544)|1. An application structure for improving the carbon sequestration effect of soil for crushing, mixing and returning straws to fields is characterized by comprising a moving vehicle, a frame, a cutter assembly, a driving structure and a decomposing agent adding assembly; the rack is positioned at the rear side of the moving vehicle, the cutter assembly and the rolling roller are arranged on the rack, and the cutter assembly is used for cutting up straws on soil; the decomposing agent adding assembly is arranged on the rack and comprises an adding barrel, a flexible pipe section, a hard pipe section, a lifting piece and a material scattering roller; the feeding barrel is fixedly arranged on the rack, and the bottom of the feeding barrel is sequentially connected with the flexible pipe section and the hard pipe section through a control valve; the axial direction of the material scattering roller is provided with a material scattering small hole and a feeding large hole, the two sides of the feeding large hole are provided with the material scattering small hole, and the feeding large hole is provided with a closing plate which can be opened and closed; the lifting piece is used for driving the hard pipe section to perform lifting motion and inserting the hard pipe section into the feeding punched hole for material input; the driving structure is connected with the spreading roller to drive the spreading roller to rotate, and materials in the spreading roller uniformly and slowly flow out of the spreading small holes.| (CN115843544)|In order to solve the problems in the prior art, the invention provides a technology for scattering a decomposing inoculant while crushing straws so as to improve the carbon fixation effect. The invention provides an application structure for improving the carbon sequestration effect of soil for crushing, mixing and returning straws, which comprises a moving vehicle, a frame, a cutter assembly, a driving structure and a decomposition agent adding assembly; the rack is positioned at the rear side of the moving vehicle, the cutter assembly and the rolling roller are arranged on the rack, and the cutter assembly is used for cutting up straws on soil; the decomposing inoculant adding assembly is arranged on the rack and comprises an adding barrel, a flexible pipe section, a hard pipe section, a lifting piece and a material scattering roller; the feeding barrel is fixedly arranged on the rack, and the bottom of the feeding barrel is sequentially connected with the flexible pipe section and the hard pipe section through a control valve; the material scattering roller is characterized in that a material scattering small hole and a material feeding large hole are axially arranged on the material scattering roller, the material scattering small hole is formed in the position of the two sides of the material feeding large hole, a sealing plate is hinged to the material feeding large hole, and the sealing plate is connected to the inner wall of the material scattering roller through a spring structure; the lifting piece is used for driving the hard pipe section to perform lifting motion and inserting the hard pipe section into the feeding punched hole for material input; the driving structure is connected with the spreading roller to drive the spreading roller to rotate, and materials in the spreading roller uniformly and slowly flow out of the spreading small holes.|The invention provides an application structure and a method for improving the carbon sequestration effect of soil in straw crushing, mixing and returning, wherein the application structure comprises a moving vehicle, a frame, a cutter assembly, a driving structure and a decomposition agent adding assembly; the driving structure is connected with the spreading roller to drive the spreading roller to rotate, and materials in the spreading roller uniformly and slowly flow out of the spreading small holes.|The invention relates to an application structure and a method for improving the carbon sequestration effect of soil in straw crushing and mixing returning, in particular to a technology for enhancing the effect after returning straws to the field.| (CN115843544)|STRAW(100,57)|GROUND(100,43)|CARBON SEQUESTRATION(100,31)|APPLICATION STRUCTURE(100,29)|MIXING(100,22)|SPREADING ROLLER(100,21)|CRUSHING(100,9)|STRAW CRUSHING(100,8)|SOIL CARBON SEQUESTRATION(100,2)|FEED BARREL(66,8)|DECOMPOSING INOCULANT(62,4)|CUTTER(59,17)|SMASHED STRAW(58,2)|FEED HOLE PUNCHING(55,2)|LIFTING PIECE(53,11)|SPREADER ROLLER(53,2)|RACK(52,12)|DECOMPOSITION(48,22)|CRUSHING STRAW(45,1)|LIFTING MOTION(42,6)|HARD PIPE SECTION(41,35)|MOVING VEHICLE(41,9)|ELEVATING SCREW ROD(40,10)|ROLLING ROLLER(40,7)|CHANNEL INCLINATION(36,18)|STRAW CUTTING(33,4)|BARREL ADDITION(30,6)|LIFTING CHUTE(30,6)|STRAW MIXED CRUSHING(30,1)|RETURNING STRAW(29,2)|FEEDING LARGE HOLE(27,22)|CLOSURE PLATE(27,16)|DRIVING STRUCTURE(27,9)|DOWNTHEHOLE CLEARANCE(27,2)|FLEXIBLE PIPE SECTION(26,9)|SPREADING SMALL HOLE(26,4)|MIXED STRAW(26,2)|DRIVING GEARBOX(24,6)|ECCENTRIC SWING MOTION(24,2)|DRIVEN GEAR(23,12)|LINKAGE SHAFT ROD(23,4)|MATURITY(23,4)|STABILIZING SUPPORT ROD(22,4)|NITROGENOUS FERTILIZER(19,15)|LIFTING PLATE(19,12)|ADJUSTING SCREW ROD(18,8)|CUTTING KNIFE(18,3)|STORAGE BUCKET(18,2)|CLEANING NEEDLE CONNECTION(16,5)|ECCENTRIC ROTATION(16,2)|SWINGING FRAME(16,2)|DRIVING ROTATION(15,6)|LINKAGE ROTATING ROD(15,3)|HARD TUBE SECTION(14,3)|SWING FRAME(14,3)|LIFTER PLATE(14,2)|SMALL HOLE(12,12)|ROTATING PLATE(12,6)|SEALING PLATE(12,4)|BLOCKAGE(12,3)|MACHINE FRAME(12,1)|CLOSING PLATE(11,10)|LIFTING MOVEMENT(11,5)|SCATTERING POSITION(11,4)|DRIVING CHAIN(11,3)|STRAW DECOMPOSITION(11,3)|CARBON FIXATION(11,2)|CUTTING LIFTING ROD BOTTOM(11,2)|LIFTING MEMBER(11,2)|SPRING STRUCTURE(10,3)|SOLID CARBON(10,2)|MATERIAL ROLLER(9,4)|ADDING BARREL CONNECTION(9,2)|FIXED PLATE(8,6)|FEED(8,5)|AGENT MATERIAL DECOMPOSITION(8,2)|CUTTER ASSEMBLY CUT(8,2)|LIFTING MOTOR DRIVE(8,2)|INPUT EQUIPMENT(7,5)|FLEXIBLE PIPE CONNECTION(7,4)|FLATTENING OPERATION(7,3)|DRIVING CONNECTION(7,2)|FEEDING MACROPOROUS HOLE(7,2)|Y SHAPED CHANNEL(6,5)|HINGE PIVOT(6,3)|CLEANING BRUSH(6,2)|WORKING(6,2)|STRAW CHOPPING(6,1)|LARGE FEEDING(5,7)|MATERIAL FEEDING LARGE HOLE(5,6)|MOUNTING PLATE(5,6)|INNER WALL(5,3)|MATERIAL INJECTION(5,3)|CAR GROOVE(5,2)|DRIVING MOTOR DRIVE(5,2)|MATERIAL INSTALLATION BLOCK(5,2)|ROTARY TILLAGE(5,1)|STRAW BURNING(5,1)|SWEEPING BRUSH(5,1)|CONTROL VALVE(4,8)|ROTATING(4,4)|MICROORGANISM(4,2)|CUTTING STRAW(4,1)|FEEDING BIG HOLE(4,1)|INSUFFICIENT DEGRADATION(4,1)|STRAW ACCIDENTAL MOVEMENT(4,1)| (CN115843544)|1. An application structure for improving the carbon sequestration effect of soil for crushing, mixing and returning straws to fields is characterized by comprising a moving vehicle, a frame, a cutter assembly, a driving structure and a decomposing agent adding assembly; the rack is positioned at the rear side of the moving vehicle, the cutter assembly and the rolling roller are arranged on the rack, and the cutter assembly is used for cutting up straws on soil; the decomposing agent adding assembly is arranged on the rack and comprises an adding barrel, a flexible pipe section, a hard pipe section, a lifting piece and a material scattering roller; the feeding barrel is fixedly arranged on the rack, and the bottom of the feeding barrel is sequentially connected with the flexible pipe section and the hard pipe section through a control valve; the axial direction of the material scattering roller is provided with a material scattering small hole and a feeding large hole, the two sides of the feeding large hole are provided with the material scattering small hole, and the feeding large hole is provided with a closing plate which can be opened and closed; the lifting piece is used for driving the hard pipe section to perform lifting motion and inserting the hard pipe section into the feeding punched hole for material input; the driving structure is connected with the spreading roller to drive the spreading roller to rotate, and materials in the spreading roller uniformly and slowly flow out of the spreading small holes.|2. The application structure for improving the soil carbon sequestration effect of straw mixed crushing and returning to the field according to claim 1, further comprising a nitrogen-containing fertilizer adding assembly, wherein the nitrogen-containing fertilizer adding assembly comprises an adding barrel body, a flexible pipe body and a hard pipe body which are sequentially connected, the feeding holes on the spreading roller are divided into two groups, and the lifting piece is used for driving the hard pipe body to lift and enter the spreading roller for feeding; a Y-shaped channel is formed in the material scattering roller, the Y-shaped channel is provided with a first inclined channel, a second inclined channel and a vertical channel, the upper side of the first inclined channel is provided with a feeding large hole for adding a decomposing agent, and the upper side of the second inclined channel is provided with a feeding large hole for adding a nitrogen-containing fertilizer;|a closing plate is hinged to the feeding large hole and connected to the inner wall of the material scattering roller through a spring structure; or the closing plate is electrically controlled to open and close.|3. The application structure of improving the carbon sequestration effect of soil for straw smashing, mixing and returning to the field according to claim 1, wherein the driving structure comprises a driving motor, a driving rotating plate and an adjusting screw rod, the driving motor is connected with the driving rotating plate, a chute is arranged on the driving rotating plate, the adjusting screw rod is arranged in the chute, an installation block of the material scattering roller is arranged on the adjusting screw rod, and the installation block is slidably arranged in the chute.|4. The application structure for improving the carbon sequestration effect of the soil in which the straw is smashed and mixed and returned to the field according to claim 1, wherein the lifting member comprises a fixed plate, a lifting motor, a lifting screw rod and a lifting plate, the lifting motor is arranged on the fixed plate and is in driving connection with the lifting screw rod, the lifting plate is arranged on the lifting screw rod and is slidably arranged in a lifting chute, the lifting screw rod is arranged in the lifting chute, and the hard pipe section is arranged on the lifting plate; in addition, still be provided with on the lifter plate and clean the needle body, clean the needle body and be used for inserting spill the downthehole clearance of expecting.|5. The structure of claim 1, wherein the cutter assembly comprises a driving gear box, a driving gear, a driven gear, a first cutting lifting rod, a linkage rotating rod and a second cutting lifting rod, the driving gear box is connected with the driving gear, the driving gear is connected with the driven gear through a driving chain, the first cutting lifting rod is eccentrically connected with the first side of the driven gear, the second side of the driven gear is connected with the linkage shaft rod, one end of the linkage shaft rod is connected with a rotating plate, the rotating plate is eccentrically connected with the second cutting lifting rod, the bottoms of the first cutting lifting rod and the second cutting lifting rod are hinged to the driving gear, the two ends of a connecting shaft are hinged to a swinging frame, the swinging frame is connected to the stabilizing supporting rod, the stabilizing supporting rod is hinged to a machine frame, the connecting shaft is hinged to a mounting plate, and the mounting plate is fixed to the cutting knife.|6. The working method of the application structure for improving the carbon sequestration effect of the soil with the smashed and mixed straw returned to the field as claimed in claim 1, is characterized by comprising the following steps:|the moving vehicle drives the rack and the cutter assembly to move, and the cutter assembly cuts up the straws on the soil; in addition, the rolling roller is in contact with the straws and rotates to perform rolling and flattening operation on the straws on the soil;|the decomposing agent material in the feeding barrel enters the flexible pipe section and the hard pipe section under the control of the control valve, the hard pipe section is controlled by the lifting piece to perform lifting movement, namely the hard pipe section is inserted into the feeding large hole to perform material injection, the closing plate is bounced off when the hard pipe section is inserted, and the closing plate is reset when the hard pipe section leaves the feeding large hole;|the driving structure drives the material scattering roller to rotate, and the decomposing agent materials in the material scattering roller gradually come out from the material scattering small holes in the rotating process and are dispersed on the straws so as to improve the carbon sequestration effect of the soil.|7. The working method of the application structure for improving the carbon sequestration effect of the soil for straw smashing, mixing and returning to the field as claimed in claim 6, is characterized by comprising the following steps: the decomposing agent in the first inclined channel and the nitrogenous fertilizer in the second inclined channel are mixed and discharged in the vertical channel, and then move to two side positions and flow out of the small material spreading holes.|8. The working method of the application structure for improving the carbon sequestration effect of the soil with the smashed and mixed straw returned to the field as claimed in claim 6, characterized by comprising the following steps: the adjusting screw rod drives the mounting block to drive the material scattering roller to move in the chute after adjustment, so that the material scattering roller on the driving rotating plate is eccentrically arranged, the contact degree of the material scattering roller and the straw is adjusted, the driving motor drives the material scattering roller to rotate, eccentric swing motion is formed, the straw is beaten when the material scattering roller moves to a relatively low position so that the structure is compacted, and the mixing effect of nitrogen and a decomposition agent in the fertilizer is enhanced through the eccentric rotation effect of the material scattering roller.|9. The working method of the application structure for improving the carbon sequestration effect of the soil for straw smashing, mixing and returning to the field as claimed in claim 6, is characterized by comprising the following steps: the lifting motor drives the lifting screw rod to work, the lifting screw rod enables the lifting plate to perform lifting motion, so that the hard pipe section and the cleaning needle body perform lifting motion, the hard pipe section can be inserted into the large feeding hole to break the sealing plate to inject materials, the cleaning needle body moves to the position of the scattering small hole to break the position of the scattering small hole, and the blockage of the position of the scattering small hole is avoided. (CN115843544)|TECHNICAL FIELD|[0001] The invention relates to an application structure and a method for improving the carbon sequestration effect of soil in straw crushing and mixing returning, in particular to a technology for enhancing the effect after returning straws to the field.|BACKGROUND ART|[0002] The straw returning to the field generally refers to the returning to the field for recycling through the straws, which is a measure for improving the soil fertility recognized in the world, and the method can obviously reduce the straw burning, thereby avoiding the atmospheric pollution. The main functions of straw returning are to increase the organic matter content of soil and improve the soil structure, so that the soil is loosened, the porosity is increased, and the capacity of the soil is reduced. In addition, the activity of the microorganism can be improved, and the root system development can be promoted.|[0003] However, if relying solely on straw chopping for returning to the field, the effect is not significant because of insufficient degradation and corrosion rate; therefore, after the existing straws are crushed and returned to the field, the straw decomposition agent is additionally applied according to the needs, and the material can enable the organic wastes in the straws to be decomposed and decomposed more quickly, so that the organic matters contained in the straws can be quickly formed into the nutrition for plant growth, beneficial microorganisms can be generated, and the crop production can be promoted.|[0004] However, in the existing structural device for returning straws to fields, the function is single, only the effect of cutting straws and returning the straws to the fields is achieved, the straw decomposition agent cannot be applied in the process at the same time, and the degradation rate of organic matters is slow, so that the carbon sequestration effect on soil is obviously influenced. If the decomposition agent is used after the straws are returned to the field, on one hand, the working strength is improved, and because partial straws are buried in the surface layer of the soil by subsequent rotary tillage, the effect of adding the decomposition agent subsequently is not good generally, and if the decomposition agent can be added while the straws are broken and returned to the field, the decomposition efficiency can be ensured to the maximum extent, so that the carbon sequestration effect of the soil is improved, and the working strength is reduced.|DISCLOSURE|Disclosure of Invention|[0005] In order to solve the problems in the prior art, the invention provides a technology for scattering a decomposing inoculant while crushing straws so as to improve the carbon fixation effect.|[0006] The invention provides an application structure for improving the carbon sequestration effect of soil for crushing, mixing and returning straws, which comprises a moving vehicle, a frame, a cutter assembly, a driving structure and a decomposition agent adding assembly; the rack is positioned at the rear side of the moving vehicle, the cutter assembly and the rolling roller are arranged on the rack, and the cutter assembly is used for cutting up straws on soil; the decomposing inoculant adding assembly is arranged on the rack and comprises an adding barrel, a flexible pipe section, a hard pipe section, a lifting piece and a material scattering roller; the feeding barrel is fixedly arranged on the rack, and the bottom of the feeding barrel is sequentially connected with the flexible pipe section and the hard pipe section through a control valve; the material scattering roller is characterized in that a material scattering small hole and a material feeding large hole are axially arranged on the material scattering roller, the material scattering small hole is formed in the position of the two sides of the material feeding large hole, a sealing plate is hinged to the material feeding large hole, and the sealing plate is connected to the inner wall of the material scattering roller through a spring structure; the lifting piece is used for driving the hard pipe section to perform lifting motion and inserting the hard pipe section into the feeding punched hole for material input; the driving structure is connected with the spreading roller to drive the spreading roller to rotate, and materials in the spreading roller uniformly and slowly flow out of the spreading small holes.|[0007] The beneficial effect of above-mentioned scheme does: when carrying out the straw cutting, put into the maturity agent material through adding the storage bucket and spill the material roller in, spill the material roller and can slowly evenly spill the straw to the material through rotating the effect, can realize like this that the straw cutting is broken simultaneously and trade the field and the purpose that the maturity agent material adds, not only simplified working process but also improved the solid carbon effect that the straw was returned to the field, had fine application effect.|[0008] Preferably, the device further comprises a nitrogen-containing fertilizer adding assembly, wherein the nitrogen-containing fertilizer adding assembly is provided with an adding barrel body, a flexible pipe body and a hard pipe body which are sequentially connected, feeding holes on the spreading roller are divided into two groups, and the lifting piece is used for driving the hard pipe body to lift and enter the spreading roller for material input; a Y-shaped channel is formed in the material scattering roller and provided with a first inclined channel, a second inclined channel and a vertical channel, the upper side of the first inclined channel is provided with a feeding macroporous hole for adding a decomposing agent, and the upper side of the second inclined channel is provided with a feeding macroporous hole for adding a nitrogen-containing fertilizer.|[0009] Here can add two kinds of materials simultaneously, be decomposition agent and nitrogenous material respectively, both can mix, spills the material after mixing like this, has better application effect.|[0010] Preferably, the driving structure comprises a driving motor, a driving rotating plate and an adjusting screw rod, the driving motor is connected with the driving rotating plate, a chute is formed in the driving rotating plate, the adjusting screw rod is arranged in the chute, an installation block of the material scattering roller is arranged on the adjusting screw rod, and the installation block is slidably arranged in the chute.|[0011] In specific application, the material scattering roller is used for rotating and scattering materials, and can hit the structure most and actively hit and compact the straws on the soil in further application, namely the material scattering roller is driven by a driving motor to rotate in a swinging mode and hit and compact the straws below at a relatively low position, so that the material scattering roller can well compress and flatten the straws in cooperation with the rolling roller, subsequent cutting operation is facilitated better, and accidental movement of the straws is avoided.|[0012] Preferably, the lifting piece comprises a fixed plate, a lifting motor, a lifting screw rod and a lifting plate, the lifting motor is arranged on the fixed plate and is in driving connection with the lifting screw rod, the lifting plate is arranged on the lifting screw rod and is slidably arranged in a lifting chute, the lifting screw rod is arranged in the lifting chute, and the hard pipe section is arranged on the lifting plate; in addition, still be provided with on the lifter plate and clean the needle body, clean the needle body and be used for inserting spill the downthehole clearance of expecting.|[0013] When the spreading roller is used for beating operation or is in contact with straws, the problem that the spreading small holes are blocked possibly occurs, and the fast cleaning action of the blocked holes is realized by simultaneously inserting and cleaning during feeding.|[0014] In addition, the cleaning needle body can also be set as a cleaning brush, and the cleaning brush can be continuously contacted with the spreading roller, namely the spreading roller can be continuously contacted with the sweeping brush in the rotating process, namely the cleaning action is realized in the spreading process, so that the cleanability of the small spreading holes is kept.|[0015] Preferably, the cutter assembly is provided with a driving gearbox, a driving gear, a driven gear, a first cutting lifting rod, a linkage rotating rod and a second cutting lifting rod, the driving gearbox is connected with the driving gear, the driving gear is connected with the driven gear through a driving chain, the first cutting lifting rod is eccentrically connected with the first side of the driven gear, the second side of the driven gear is connected with the linkage shaft rod, one end of the linkage shaft rod is connected with a rotating plate, the second cutting lifting rod is eccentrically connected with the rotating plate, the bottoms of the first cutting lifting rod and the second cutting lifting rod are hinged on the connecting shaft, two ends of the connecting shaft are hinged on a swinging frame, the swinging frame is connected on the stable supporting rod, the stable supporting rod is hinged on the rack, the connecting shaft is hinged on a mounting plate, and the mounting plate is fixed on the cutting knife.|[0016] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field provided by the invention comprises the following steps:|[0017] the moving vehicle drives the rack and the cutter assembly to move, and the cutter assembly cuts up the straws on the soil; in addition, the rolling roller is in contact with the straws and rotates to perform rolling and flattening operation on the straws on the soil;|[0018] the decomposing agent material in the feeding barrel enters the flexible pipe section and the hard pipe section under the control of the control valve, the hard pipe section is controlled by the lifting piece to perform lifting movement, namely the hard pipe section is inserted into the feeding large hole to perform material injection, the closing plate is bounced off when the hard pipe section is inserted, and the closing plate is reset when the hard pipe section leaves the feeding large hole;|[0019] the driving structure drives the material scattering roller to rotate, and in the rotating process, the decomposing agent materials in the material scattering roller gradually come out from the material scattering small holes and are dispersed on the straws so as to improve the carbon fixation effect of the soil.|[0020] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: the decomposing agent in the first inclined channel and the nitrogenous fertilizer in the second inclined channel are mixed and discharged in the vertical channel, and then move to two side positions and flow out of the small material spreading holes.|[0021] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: the adjusting screw rod drives the mounting block to drive the material scattering roller to move in the chute after adjustment, so that the material scattering roller on the driving rotating plate is eccentrically arranged, the contact degree of the material scattering roller and the straw is adjusted, the driving motor drives the material scattering roller to rotate, eccentric swing motion is formed, the straw is beaten when the material scattering roller moves to a relatively low position so that the structure is compacted, and the mixing effect of nitrogen and a decomposition agent in the fertilizer is enhanced through the eccentric rotation effect of the material scattering roller.|[0022] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: the lifting motor drives the lifting screw rod to work, the lifting screw rod enables the lifting plate to perform lifting motion, so that the hard pipe section and the cleaning needle body perform lifting motion, the hard pipe section can be inserted into the large feeding hole to break the sealing plate to inject materials, the cleaning needle body moves to the position of the scattering small hole to break the position of the scattering small hole, and the blockage of the position of the scattering small hole is avoided.|DRAWINGS DESCRIPTION|[0023] FIG. 1 is a schematic structural diagram of an application structure for improving the carbon sequestration effect of soil in straw crushing, mixing and returning to the field;|[0024] FIG. 2 is a partial structural diagram of an application structure for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field according to the present invention;|[0025] FIG. 3 is a schematic structural diagram of a partial side sectional view of an application structure of the present invention for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field;|[0026] FIG. 4 is an enlarged structural view of the area A in FIG. 3;|[0027] FIG. 5 is a schematic structural diagram of a plan view in the spreading roller of an application structure for improving the carbon sequestration effect of the soil in which the straws are smashed, mixed and returned to the field according to the invention;|[0028] FIG. 6 is a partial structural diagram of an application structure for improving the carbon sequestration effect of soil in the field of straw crushing and mixing and returning to the field;|[0029] FIG. 7 is a partial structural diagram of an application structure of the present invention for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field;|[0030] FIG. 8 is a partial structural diagram of an application structure of the present invention for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field;|[0031] FIG. 9 is a partial structural diagram of an application structure of the present invention for improving the carbon sequestration effect of soil in the field of straw crushing and mixing;|[0032] FIG. 10 is an enlarged structural view of the area B in FIG. 8;|[0033] FIG. 11 is a partial structural diagram of an application structure of the present invention for improving the carbon sequestration effect of soil in the field of straw crushing and returning to the field.|INVENTION MODE|Detailed Description|[0034] The first embodiment:|[0035] as shown in fig. 1 to 4, the present embodiment provides an application structure for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field. The device comprises a moving vehicle 10, a frame 20, a cutter assembly 30, a driving structure 40 and a decomposing agent adding assembly 50; the frame 20 is positioned at the rear side of the mobile vehicle 10, the cutter assembly 30 and the rolling roller 21 are arranged on the frame 20, and the cutter assembly 30 is used for cutting up the straws on the soil; the decomposing inoculant adding assembly 50 is arranged on the rack 20, and the decomposing inoculant adding assembly 50 comprises an adding barrel 51, a flexible pipe section 52, a hard pipe section 53, a lifting piece 60 and a spreading roller 70; the feeding barrel 51 is fixedly arranged on the frame 10, and the bottom of the feeding barrel 51 is sequentially connected with the flexible pipe section 52 and the hard pipe section 53 through a control valve 54; a material scattering small hole 71 and a material feeding large hole 72 are arranged on the material scattering roller 70 in the axial direction, the material scattering small hole 71 is arranged at the position of two sides of the material feeding large hole 72, and a closing plate 73 capable of being opened and closed is arranged at the position of the material feeding large hole 72; for example, a closing plate 73 is hinged on the feeding big hole 72, and the closing plate 73 is connected to a vertical plate 151 on the inner wall of the scattering roller 70 through a spring structure 74; or the closing plate is a closing plate controlled by electric opening and closing, for example, the closing plate is connected to the feeding large hole through a hinge pivot, the opening and closing of the feeding large hole by the closing plate are controlled by the rotation drive of the hinge pivot, for example, the rotation of the hinge pivot can be realized by the drive of a motor.|[0036] The lifting piece 60 is used for driving the hard pipe section 53 to perform lifting movement and inserting the hard pipe section into the large feeding hole 72 for material input; the driving structure 40 is connected with the spreading roller 71 to drive and rotate, and the material in the spreading roller 71 uniformly and slowly flows out of the spreading small holes 71.|[0037] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field provided by the invention comprises the following steps:|[0038] the moving vehicle 10 drives the frame 20 and the cutter assembly 30 to move, and the cutter assembly 30 cuts up the straws on the soil; in addition, the rolling roller 21 is in contact with the straw and rotates to perform rolling and flattening operation on the straw on the soil;|[0039] the decomposing agent material in the adding barrel 51 enters the flexible pipe section 52 and the hard pipe section 53 under the control of the control valve 54, the hard pipe section 53 is lifted under the control of the lifting piece 60, namely, the hard pipe section 53 is inserted into the feeding large hole 72 for injecting the material, the hard pipe section 53 is inserted, the closing plate 74 is bounced off, and the closing plate 73 is reset when the hard pipe section 53 leaves the feeding large hole 72;|[0040] the driving structure 40 drives the material spreading roller 70 to rotate, so that the decomposition agent materials in the material spreading roller 70 gradually come out from the material spreading small holes 71 and are dispersed on the straws in the rotating process to improve the soil carbon fixation effect.|[0041] After the hard tube leaves the closing plate, the hard tube is reset under the action of the spring so as to drive the closing plate to reset and form a closed state.|[0042] The hard tube section is inserted into the spreader roller when it is desired to feed, the closure plate is opened when it is not desired to remove the hard tube section when feeding is desired, and the closure plate is closed and the spreader roller is rotated to spread the material.|[0043] Second embodiment:|[0044] as shown in fig. 2 and 5, the fertilizer adding device further comprises a nitrogen-containing fertilizer adding assembly 80, wherein the nitrogen-containing fertilizer adding assembly 80 comprises an adding barrel 81, a flexible pipe body 101 and a hard pipe body 82 which are connected in sequence, and a control valve controls materials in the adding barrel 81 to enter the flexible pipe body and the hard pipe body. Two groups of large feeding holes 72 are formed in the material scattering roller 70, and the lifting piece 60 is used for driving the hard pipe body 82 to lift and enter the material scattering roller 70 for material input; a Y-shaped channel 83 is formed in the material scattering roller 70, the Y-shaped channel 83 is provided with a first inclined channel 84, a second inclined channel 85 and a vertical channel 86, the upper side of the first inclined channel 84 is provided with a large feeding hole 72 for adding the decomposing agent, and the upper side of the second inclined channel 85 is provided with a large feeding hole 72 for adding the nitrogen-containing fertilizer. The invention provides a working method of an application structure for improving the carbon sequestration effect of soil in straw crushing, mixing and returning, which comprises the following steps: the decomposition agent in the first inclined channel 84 and the nitrogen-containing fertilizer in the second inclined channel 85 are mixed and fed in the vertical channel 86, and then move to two sides and flow out of the material spreading small holes 71.|[0045] As shown in fig. 6, the driving structure 40 includes a driving motor 41, a driving rotating plate 42, and an adjusting screw 43, the driving motor 41 is connected to the driving rotating plate 42, a sliding slot 44 is disposed on the driving rotating plate 42, the adjusting screw 43 is disposed in the sliding slot 44, an installation block 45 of the material spreading roller 70 is disposed on the adjusting screw 43, and the installation block 45 is slidably disposed in the sliding slot 44. The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: after the adjusting screw 43 is adjusted, the mounting block 45 drives the material scattering roller 70 to move in the chute 44, so that the material scattering roller 70 on the driving rotating plate 42 is eccentrically arranged, the contact degree of the material scattering roller 70 and the straw is adjusted, the driving motor 41 drives the material scattering roller 70 to rotate, eccentric swinging motion is formed, when the material scattering roller 70 moves to a relatively low position, the straw is beaten to compact the structure, and the mixing effect of the nitrogen-containing fertilizer and the decomposition agent is enhanced through the eccentric rotating effect of the material scattering roller 70.|[0046] The third embodiment:|[0047] as shown in fig. 7, the lifting member 60 of this embodiment includes a fixing plate 61, a lifting motor 62, a lifting screw 63 and a lifting plate 64, the lifting motor 62 is disposed on the fixing plate 61, the lifting motor 62 is drivingly connected to the lifting screw 63, the lifting plate 61 is disposed on the lifting screw 63, the lifting plate 61 is slidably disposed in a lifting chute 65, the lifting screw 63 is disposed in the lifting chute 65, and the hard tube section 53 is disposed on the lifting plate 64; in addition, the lifting plate 64 is further provided with a cleaning needle 66, and the cleaning needle 66 is inserted into the scattering small hole 71 for cleaning.|[0048] As shown in fig. 8 to 11, the cutter assembly 30 includes a driving gear box 31, a driving gear 32, a driven gear 33, a first cutting lifting rod 34, a linkage rotating rod 35, and a second cutting lifting rod 36, the driving gear box 31 is connected to the driving gear 32, the driving gear 32 is connected to the driven gear 33 through a driving chain 37, a first cutting lifting rod 34 is eccentrically connected to a first side of the driven gear 33, a second side of the driven gear 33 is connected to the linkage shaft 35, one end of the linkage shaft 35 is connected to a rotating plate 38, the second cutting lifting rod 36 is eccentrically connected to the rotating plate 38, bottoms of the first cutting lifting rod 34 and the second cutting lifting rod 36 are hinged to the connecting shaft 39, both ends of the connecting shaft 39 are hinged to a swing frame 91, the swing frame 91 is connected to the stabilizing support rod 92, the stabilizing support rod 92 is hinged to the machine frame 20, the connecting shaft 39 is hinged to a mounting plate 93, and the mounting plate 93 is fixed to the cutting knife 94.|[0049] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: the lifting motor 62 drives the lifting screw 63 to work, the lifting screw 63 enables the lifting plate 64 to perform lifting movement, so that the hard pipe section 53 and the cleaning needle 66 perform lifting movement, the hard pipe section 53 is inserted into the large feeding hole 72 to break the closing plate 73 for injecting materials, and the cleaning needle 66 moves to the position of the material scattering small hole 71 and breaks the position of the material scattering small hole 71, so as to avoid the blockage of the position of the material scattering small hole 71.|[0050] It is to be noted that both the straw decomposition agent and the nitrogen-containing fertilizer are in the prior art, and for example, urea is used as the nitrogen-containing fertilizer. The control valve may be a manual valve or an electrically operated valve. In addition, the closing plate can be an electric plate, namely the closing plate is controlled to be automatically opened or closed in an electric mode, and after the closing plate is opened, the hard pipe can be inserted into the spreading roller. For example, a sliding groove is formed in the position of the feeding large hole, a slidable closing plate is arranged in the sliding groove, the closing plate is controlled through a telescopic cylinder, the telescopic cylinder is used for closing or opening the feeding large hole through controlling the closing plate, and the closing plate can be opened and closed under the state. (CN115843544)|TECHNICAL FIELD|[0001] The invention relates to an application structure and a method for improving the carbon sequestration effect of soil in straw crushing and mixing returning, in particular to a technology for enhancing the effect after returning straws to the field.|BACKGROUND ART|[0002] The straw returning to the field generally refers to the returning to the field for recycling through the straws, which is a measure for improving the soil fertility recognized in the world, and the method can obviously reduce the straw burning, thereby avoiding the atmospheric pollution. The main functions of straw returning are to increase the organic matter content of soil and improve the soil structure, so that the soil is loosened, the porosity is increased, and the capacity of the soil is reduced. In addition, the activity of the microorganism can be improved, and the root system development can be promoted.|[0003] However, if relying solely on straw chopping for returning to the field, the effect is not significant because of insufficient degradation and corrosion rate; therefore, after the existing straws are crushed and returned to the field, the straw decomposition agent is additionally applied according to the needs, and the material can enable the organic wastes in the straws to be decomposed and decomposed more quickly, so that the organic matters contained in the straws can be quickly formed into the nutrition for plant growth, beneficial microorganisms can be generated, and the crop production can be promoted.|[0004] However, in the existing structural device for returning straws to fields, the function is single, only the effect of cutting straws and returning the straws to the fields is achieved, the straw decomposition agent cannot be applied in the process at the same time, and the degradation rate of organic matters is slow, so that the carbon sequestration effect on soil is obviously influenced. If the decomposition agent is used after the straws are returned to the field, on one hand, the working strength is improved, and because partial straws are buried in the surface layer of the soil by subsequent rotary tillage, the effect of adding the decomposition agent subsequently is not good generally, and if the decomposition agent can be added while the straws are broken and returned to the field, the decomposition efficiency can be ensured to the maximum extent, so that the carbon sequestration effect of the soil is improved, and the working strength is reduced.|DISCLOSURE|Disclosure of Invention|[0005] In order to solve the problems in the prior art, the invention provides a technology for scattering a decomposing inoculant while crushing straws so as to improve the carbon fixation effect.|[0006] The invention provides an application structure for improving the carbon sequestration effect of soil for crushing, mixing and returning straws, which comprises a moving vehicle, a frame, a cutter assembly, a driving structure and a decomposition agent adding assembly; the rack is positioned at the rear side of the moving vehicle, the cutter assembly and the rolling roller are arranged on the rack, and the cutter assembly is used for cutting up straws on soil; the decomposing inoculant adding assembly is arranged on the rack and comprises an adding barrel, a flexible pipe section, a hard pipe section, a lifting piece and a material scattering roller; the feeding barrel is fixedly arranged on the rack, and the bottom of the feeding barrel is sequentially connected with the flexible pipe section and the hard pipe section through a control valve; the material scattering roller is characterized in that a material scattering small hole and a material feeding large hole are axially arranged on the material scattering roller, the material scattering small hole is formed in the position of the two sides of the material feeding large hole, a sealing plate is hinged to the material feeding large hole, and the sealing plate is connected to the inner wall of the material scattering roller through a spring structure; the lifting piece is used for driving the hard pipe section to perform lifting motion and inserting the hard pipe section into the feeding punched hole for material input; the driving structure is connected with the spreading roller to drive the spreading roller to rotate, and materials in the spreading roller uniformly and slowly flow out of the spreading small holes.|[0007] The beneficial effect of above-mentioned scheme does: when carrying out the straw cutting, put into the maturity agent material through adding the storage bucket and spill the material roller in, spill the material roller and can slowly evenly spill the straw to the material through rotating the effect, can realize like this that the straw cutting is broken simultaneously and trade the field and the purpose that the maturity agent material adds, not only simplified working process but also improved the solid carbon effect that the straw was returned to the field, had fine application effect.|[0008] Preferably, the device further comprises a nitrogen-containing fertilizer adding assembly, wherein the nitrogen-containing fertilizer adding assembly is provided with an adding barrel body, a flexible pipe body and a hard pipe body which are sequentially connected, feeding holes on the spreading roller are divided into two groups, and the lifting piece is used for driving the hard pipe body to lift and enter the spreading roller for material input; a Y-shaped channel is formed in the material scattering roller and provided with a first inclined channel, a second inclined channel and a vertical channel, the upper side of the first inclined channel is provided with a feeding macroporous hole for adding a decomposing agent, and the upper side of the second inclined channel is provided with a feeding macroporous hole for adding a nitrogen-containing fertilizer.|[0009] Here can add two kinds of materials simultaneously, be decomposition agent and nitrogenous material respectively, both can mix, spills the material after mixing like this, has better application effect.|[0010] Preferably, the driving structure comprises a driving motor, a driving rotating plate and an adjusting screw rod, the driving motor is connected with the driving rotating plate, a chute is formed in the driving rotating plate, the adjusting screw rod is arranged in the chute, an installation block of the material scattering roller is arranged on the adjusting screw rod, and the installation block is slidably arranged in the chute.|[0011] In specific application, the material scattering roller is used for rotating and scattering materials, and can hit the structure most and actively hit and compact the straws on the soil in further application, namely the material scattering roller is driven by a driving motor to rotate in a swinging mode and hit and compact the straws below at a relatively low position, so that the material scattering roller can well compress and flatten the straws in cooperation with the rolling roller, subsequent cutting operation is facilitated better, and accidental movement of the straws is avoided.|[0012] Preferably, the lifting piece comprises a fixed plate, a lifting motor, a lifting screw rod and a lifting plate, the lifting motor is arranged on the fixed plate and is in driving connection with the lifting screw rod, the lifting plate is arranged on the lifting screw rod and is slidably arranged in a lifting chute, the lifting screw rod is arranged in the lifting chute, and the hard pipe section is arranged on the lifting plate; in addition, still be provided with on the lifter plate and clean the needle body, clean the needle body and be used for inserting spill the downthehole clearance of expecting.|[0013] When the spreading roller is used for beating operation or is in contact with straws, the problem that the spreading small holes are blocked possibly occurs, and the fast cleaning action of the blocked holes is realized by simultaneously inserting and cleaning during feeding.|[0014] In addition, the cleaning needle body can also be set as a cleaning brush, and the cleaning brush can be continuously contacted with the spreading roller, namely the spreading roller can be continuously contacted with the sweeping brush in the rotating process, namely the cleaning action is realized in the spreading process, so that the cleanability of the small spreading holes is kept.|[0015] Preferably, the cutter assembly is provided with a driving gearbox, a driving gear, a driven gear, a first cutting lifting rod, a linkage rotating rod and a second cutting lifting rod, the driving gearbox is connected with the driving gear, the driving gear is connected with the driven gear through a driving chain, the first cutting lifting rod is eccentrically connected with the first side of the driven gear, the second side of the driven gear is connected with the linkage shaft rod, one end of the linkage shaft rod is connected with a rotating plate, the second cutting lifting rod is eccentrically connected with the rotating plate, the bottoms of the first cutting lifting rod and the second cutting lifting rod are hinged on the connecting shaft, two ends of the connecting shaft are hinged on a swinging frame, the swinging frame is connected on the stable supporting rod, the stable supporting rod is hinged on the rack, the connecting shaft is hinged on a mounting plate, and the mounting plate is fixed on the cutting knife.|[0016] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field provided by the invention comprises the following steps:|[0017] the moving vehicle drives the rack and the cutter assembly to move, and the cutter assembly cuts up the straws on the soil; in addition, the rolling roller is in contact with the straws and rotates to perform rolling and flattening operation on the straws on the soil;|[0018] the decomposing agent material in the feeding barrel enters the flexible pipe section and the hard pipe section under the control of the control valve, the hard pipe section is controlled by the lifting piece to perform lifting movement, namely the hard pipe section is inserted into the feeding large hole to perform material injection, the closing plate is bounced off when the hard pipe section is inserted, and the closing plate is reset when the hard pipe section leaves the feeding large hole;|[0019] the driving structure drives the material scattering roller to rotate, and in the rotating process, the decomposing agent materials in the material scattering roller gradually come out from the material scattering small holes and are dispersed on the straws so as to improve the carbon fixation effect of the soil.|[0020] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: the decomposing agent in the first inclined channel and the nitrogenous fertilizer in the second inclined channel are mixed and discharged in the vertical channel, and then move to two side positions and flow out of the small material spreading holes.|[0021] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: the adjusting screw rod drives the mounting block to drive the material scattering roller to move in the chute after adjustment, so that the material scattering roller on the driving rotating plate is eccentrically arranged, the contact degree of the material scattering roller and the straw is adjusted, the driving motor drives the material scattering roller to rotate, eccentric swing motion is formed, the straw is beaten when the material scattering roller moves to a relatively low position so that the structure is compacted, and the mixing effect of nitrogen and a decomposition agent in the fertilizer is enhanced through the eccentric rotation effect of the material scattering roller.|[0022] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: the lifting motor drives the lifting screw rod to work, the lifting screw rod enables the lifting plate to perform lifting motion, so that the hard pipe section and the cleaning needle body perform lifting motion, the hard pipe section can be inserted into the large feeding hole to break the sealing plate to inject materials, the cleaning needle body moves to the position of the scattering small hole to break the position of the scattering small hole, and the blockage of the position of the scattering small hole is avoided.|DRAWINGS DESCRIPTION|[0023] FIG. 1 is a schematic structural diagram of an application structure for improving the carbon sequestration effect of soil in straw crushing, mixing and returning to the field;|[0024] FIG. 2 is a partial structural diagram of an application structure for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field according to the present invention;|[0025] FIG. 3 is a schematic structural diagram of a partial side sectional view of an application structure of the present invention for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field;|[0026] FIG. 4 is an enlarged structural view of the area A in FIG. 3;|[0027] FIG. 5 is a schematic structural diagram of a plan view in the spreading roller of an application structure for improving the carbon sequestration effect of the soil in which the straws are smashed, mixed and returned to the field according to the invention;|[0028] FIG. 6 is a partial structural diagram of an application structure for improving the carbon sequestration effect of soil in the field of straw crushing and mixing and returning to the field;|[0029] FIG. 7 is a partial structural diagram of an application structure of the present invention for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field;|[0030] FIG. 8 is a partial structural diagram of an application structure of the present invention for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field;|[0031] FIG. 9 is a partial structural diagram of an application structure of the present invention for improving the carbon sequestration effect of soil in the field of straw crushing and mixing;|[0032] FIG. 10 is an enlarged structural view of the area B in FIG. 8;|[0033] FIG. 11 is a partial structural diagram of an application structure of the present invention for improving the carbon sequestration effect of soil in the field of straw crushing and returning to the field.|INVENTION MODE|Detailed Description|[0034] The first embodiment:|[0035] as shown in fig. 1 to 4, the present embodiment provides an application structure for improving the carbon sequestration effect of soil in which straw is crushed, mixed and returned to the field. The device comprises a moving vehicle 10, a frame 20, a cutter assembly 30, a driving structure 40 and a decomposing agent adding assembly 50; the frame 20 is positioned at the rear side of the mobile vehicle 10, the cutter assembly 30 and the rolling roller 21 are arranged on the frame 20, and the cutter assembly 30 is used for cutting up the straws on the soil; the decomposing inoculant adding assembly 50 is arranged on the rack 20, and the decomposing inoculant adding assembly 50 comprises an adding barrel 51, a flexible pipe section 52, a hard pipe section 53, a lifting piece 60 and a spreading roller 70; the feeding barrel 51 is fixedly arranged on the frame 10, and the bottom of the feeding barrel 51 is sequentially connected with the flexible pipe section 52 and the hard pipe section 53 through a control valve 54; a material scattering small hole 71 and a material feeding large hole 72 are arranged on the material scattering roller 70 in the axial direction, the material scattering small hole 71 is arranged at the position of two sides of the material feeding large hole 72, and a closing plate 73 capable of being opened and closed is arranged at the position of the material feeding large hole 72; for example, a closing plate 73 is hinged on the feeding big hole 72, and the closing plate 73 is connected to a vertical plate 151 on the inner wall of the scattering roller 70 through a spring structure 74; or the closing plate is a closing plate controlled by electric opening and closing, for example, the closing plate is connected to the feeding large hole through a hinge pivot, the opening and closing of the feeding large hole by the closing plate are controlled by the rotation drive of the hinge pivot, for example, the rotation of the hinge pivot can be realized by the drive of a motor.|[0036] The lifting piece 60 is used for driving the hard pipe section 53 to perform lifting movement and inserting the hard pipe section into the large feeding hole 72 for material input; the driving structure 40 is connected with the spreading roller 71 to drive and rotate, and the material in the spreading roller 71 uniformly and slowly flows out of the spreading small holes 71.|[0037] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field provided by the invention comprises the following steps:|[0038] the moving vehicle 10 drives the frame 20 and the cutter assembly 30 to move, and the cutter assembly 30 cuts up the straws on the soil; in addition, the rolling roller 21 is in contact with the straw and rotates to perform rolling and flattening operation on the straw on the soil;|[0039] the decomposing agent material in the adding barrel 51 enters the flexible pipe section 52 and the hard pipe section 53 under the control of the control valve 54, the hard pipe section 53 is lifted under the control of the lifting piece 60, namely, the hard pipe section 53 is inserted into the feeding large hole 72 for injecting the material, the hard pipe section 53 is inserted, the closing plate 74 is bounced off, and the closing plate 73 is reset when the hard pipe section 53 leaves the feeding large hole 72;|[0040] the driving structure 40 drives the material spreading roller 70 to rotate, so that the decomposition agent materials in the material spreading roller 70 gradually come out from the material spreading small holes 71 and are dispersed on the straws in the rotating process to improve the soil carbon fixation effect.|[0041] After the hard tube leaves the closing plate, the hard tube is reset under the action of the spring so as to drive the closing plate to reset and form a closed state.|[0042] The hard tube section is inserted into the spreader roller when it is desired to feed, the closure plate is opened when it is not desired to remove the hard tube section when feeding is desired, and the closure plate is closed and the spreader roller is rotated to spread the material.|[0043] Second embodiment:|[0044] as shown in fig. 2 and 5, the fertilizer adding device further comprises a nitrogen-containing fertilizer adding assembly 80, wherein the nitrogen-containing fertilizer adding assembly 80 comprises an adding barrel 81, a flexible pipe body 101 and a hard pipe body 82 which are connected in sequence, and a control valve controls materials in the adding barrel 81 to enter the flexible pipe body and the hard pipe body. Two groups of large feeding holes 72 are formed in the material scattering roller 70, and the lifting piece 60 is used for driving the hard pipe body 82 to lift and enter the material scattering roller 70 for material input; a Y-shaped channel 83 is formed in the material scattering roller 70, the Y-shaped channel 83 is provided with a first inclined channel 84, a second inclined channel 85 and a vertical channel 86, the upper side of the first inclined channel 84 is provided with a large feeding hole 72 for adding the decomposing agent, and the upper side of the second inclined channel 85 is provided with a large feeding hole 72 for adding the nitrogen-containing fertilizer. The invention provides a working method of an application structure for improving the carbon sequestration effect of soil in straw crushing, mixing and returning, which comprises the following steps: the decomposition agent in the first inclined channel 84 and the nitrogen-containing fertilizer in the second inclined channel 85 are mixed and fed in the vertical channel 86, and then move to two sides and flow out of the material spreading small holes 71.|[0045] As shown in fig. 6, the driving structure 40 includes a driving motor 41, a driving rotating plate 42, and an adjusting screw 43, the driving motor 41 is connected to the driving rotating plate 42, a sliding slot 44 is disposed on the driving rotating plate 42, the adjusting screw 43 is disposed in the sliding slot 44, an installation block 45 of the material spreading roller 70 is disposed on the adjusting screw 43, and the installation block 45 is slidably disposed in the sliding slot 44. The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: after the adjusting screw 43 is adjusted, the mounting block 45 drives the material scattering roller 70 to move in the chute 44, so that the material scattering roller 70 on the driving rotating plate 42 is eccentrically arranged, the contact degree of the material scattering roller 70 and the straw is adjusted, the driving motor 41 drives the material scattering roller 70 to rotate, eccentric swinging motion is formed, when the material scattering roller 70 moves to a relatively low position, the straw is beaten to compact the structure, and the mixing effect of the nitrogen-containing fertilizer and the decomposition agent is enhanced through the eccentric rotating effect of the material scattering roller 70.|[0046] The third embodiment:|[0047] as shown in fig. 7, the lifting member 60 of this embodiment includes a fixing plate 61, a lifting motor 62, a lifting screw 63 and a lifting plate 64, the lifting motor 62 is disposed on the fixing plate 61, the lifting motor 62 is drivingly connected to the lifting screw 63, the lifting plate 61 is disposed on the lifting screw 63, the lifting plate 61 is slidably disposed in a lifting chute 65, the lifting screw 63 is disposed in the lifting chute 65, and the hard tube section 53 is disposed on the lifting plate 64; in addition, the lifting plate 64 is further provided with a cleaning needle 66, and the cleaning needle 66 is inserted into the scattering small hole 71 for cleaning.|[0048] As shown in fig. 8 to 11, the cutter assembly 30 includes a driving gear box 31, a driving gear 32, a driven gear 33, a first cutting lifting rod 34, a linkage rotating rod 35, and a second cutting lifting rod 36, the driving gear box 31 is connected to the driving gear 32, the driving gear 32 is connected to the driven gear 33 through a driving chain 37, a first cutting lifting rod 34 is eccentrically connected to a first side of the driven gear 33, a second side of the driven gear 33 is connected to the linkage shaft 35, one end of the linkage shaft 35 is connected to a rotating plate 38, the second cutting lifting rod 36 is eccentrically connected to the rotating plate 38, bottoms of the first cutting lifting rod 34 and the second cutting lifting rod 36 are hinged to the connecting shaft 39, both ends of the connecting shaft 39 are hinged to a swing frame 91, the swing frame 91 is connected to the stabilizing support rod 92, the stabilizing support rod 92 is hinged to the machine frame 20, the connecting shaft 39 is hinged to a mounting plate 93, and the mounting plate 93 is fixed to the cutting knife 94.|[0049] The working method of the application structure for improving the carbon sequestration effect of the soil for crushing, mixing and returning the straws to the field comprises the following steps: the lifting motor 62 drives the lifting screw 63 to work, the lifting screw 63 enables the lifting plate 64 to perform lifting movement, so that the hard pipe section 53 and the cleaning needle 66 perform lifting movement, the hard pipe section 53 is inserted into the large feeding hole 72 to break the closing plate 73 for injecting materials, and the cleaning needle 66 moves to the position of the material scattering small hole 71 and breaks the position of the material scattering small hole 71, so as to avoid the blockage of the position of the material scattering small hole 71.|[0050] It is to be noted that both the straw decomposition agent and the nitrogen-containing fertilizer are in the prior art, and for example, urea is used as the nitrogen-containing fertilizer. The control valve may be a manual valve or an electrically operated valve. In addition, the closing plate can be an electric plate, namely the closing plate is controlled to be automatically opened or closed in an electric mode, and after the closing plate is opened, the hard pipe can be inserted into the spreading roller. For example, a sliding groove is formed in the position of the feeding large hole, a slidable closing plate is arranged in the sliding groove, the closing plate is controlled through a telescopic cylinder, the telescopic cylinder is used for closing or opening the feeding large hole through controlling the closing plate, and the closing plate can be opened and closed under the state. Family Number|(104310198)|104310198|Abstract|(CN115843544 A)|The invention provides an application structure and method for improving the soil carbon sequestration effect of straw crushing , mixing and returning . The application structure comprises a moving trolley , a rack , a cutter assembly , a driving structure and a decomposition agent adding assembly . The driving structure is connected with the material scattering roller to drive the material scattering roller to rotate , and materials in the material scattering roller evenly and slowly flow out of the small material scattering holes . When straw is cut , decomposition agent materials are put into the material scattering roller through the material adding barrel , and the material scattering roller can slowly and uniformly scatter the materials into the straw through the rotation effect , so that the purposes of cutting , crushing and field changing of the straw and adding of the decomposition agent materials can be achieved at the same time ; the working process is simplified , the carbon sequestration effect of straw returning is improved , and the good application effect is achieved . |IPC codes|(CN115843544 A)|A01B - 077/00 |A01C - 015/00 |A01D - 082/00 |Title|(CN115843544 A)|Application structure and method for improving soil carbon sequestration effect of straw crushing , mixing and returning | Other special machines A01B-077/00|A01C-015/00|A01D-082/00 A01B-077/00|A01C-015/00|A01D-082/00 CN118947344|CN117694118B CN118947344 112222087 WHO=Examiner SELF=N CAT=A|CN117694118B 108902707 WHO=Examiner SELF=N LAPSED (CN115843544)|LAPSED DEAD (CN115843544)|DEAD (CN115843544)|LEGAL DETAILS FOR CN115843544|Actual or expected expiration date=2023-09-22|Legal state=DEAD|Status=LAPSED|Event publication date=2022-12-07|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211562265|Application date=2022-12-07|Standardized application number=2022CN-1562265|Event publication date=2023-03-28|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115843544|Publication stage code=A|Publication date=2023-03-28|Standardized publication number=CN115843544|Event publication date=2023-03-28|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-04-14|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-09-22|Event code=CN/WW01|Event indicator=Neg|Event group=Event indicating Not In Force|Withdrawal of patent application after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRR+T+ZqO5np1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067076036&ekey=2293&xpn=CN115843544&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=j%252F3mybM4kHJ5hyuAsg3N0JNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN115843544)|CN (CN115843544)|NAME=HEILONGJIANG AGRICULTURAL ECONOMY VOCATIONAL College , COUNTRY=CN (CN115843544)|NAME=LIU LIJUAN;Shenyang Yinuojunke Intellectual Property Agency (General Partnership) , REG=21266 (CN115843544)|NAME=TONG SHUYUAN|NAME=DU ZHENYU|NAME=LIANG XUANHE|NAME=XU WENDONG|NAME=WANG HAILONG|NAME=SUN PINGPING|NAME=XU JIFA|NAME=WANG ZEJIA|NAME=WANG TIANYE|NAME=WANG XING|NAME=WANG XIANRUI 0 1 Titre: (CN115843544)|Application structure and method for improving soil carbon sequestration effect of straw crushing, mixing and returning Résumé: (CN115843544)|The invention provides an application structure and method for improving the soil carbon sequestration effect of straw crushing, mixing and returning. The application structure comprises a moving trolley, a rack, a cutter assembly, a driving structure and a decomposition agent adding assembly. The driving structure is connected with the material scattering roller to drive the material scattering roller to rotate, and materials in the material scattering roller evenly and slowly flow out of the small material scattering holes. When straw is cut, decomposition agent materials are put into the material scattering roller through the material adding barrel, and the material scattering roller can slowly and uniformly scatter the materials into the straw through the rotation effect, so that the purposes of cutting, crushing and field changing of the straw and adding of the decomposition agent materials can be achieved at the same time; the working process is simplified, the carbon sequestration effect of straw returning is improved, and the good application effect is achieved. 24 Abstract gpt-4o-mini no The article focuses on improving soil carbon sequestration through straw management and does not involve accelerated weathering of minerals or CO₂ capture.
24 CN202511179914 CN202511179914 CN121107390 117027433 CN121107390 A 2025-12-12 [CN121107390] 2025-08-22 2025-08-22 2025-12-12 (CN121107390)|2045-08-22 (CN121107390)|Carbon sequestration biochar and preparation method thereof (CN121107390)|The present invention discloses a carbon sequestration biochar and a preparation method thereof, the preparation method comprises: adding crushed biomass into a carbon sequestration agent solution to obtain a first mixture, the carbon sequestration agent comprising phosphoric acid and/or iron oxide; drying the first mixture, and grinding to obtain a powdery second mixture; and pyrolyzing the second mixture in an inert gas atmosphere to obtain the carbon-sequestered biochar. Therefore, the high-yield and high-carbon-content biochar is prepared through co-pyrolysis of phosphoric acid, ferric oxide and biomass, the carbon sequestration rate of the biochar is increased through the synergistic effect of phosphoric acid and ferric oxide, a physical barrier is formed on the surface of the biochar, the oxidation resistance and biomineralization resistance of the biochar are enhanced, and escape of a biomass pyrolysis primary product is limited; it is thus retained in the carbon matrix, resulting in more carbon retention and high yields. The biochar is applied to cement slurry, and all phosphorus and iron elements contained in the biochar are utilized to stimulate the hydration reaction of cement to improve the mechanical property. ANHUI CONCH BIOMASS ENERGY TECHNOLOGY|HEFEI UNIVERSITY OF TECHNOLOGY (CN121107390)|HEFEI UNIVERSITY OF TECHNOLOGY ([CN])|ANHUI CONCH BIOMASS ENERGY TECHNOLOGY CO., LTD. DIAO RUI|HU XU|LI BOWEN|YANG CUNZHANG|QI FENGLEI|LIU XIAOHAO|CHA ZHENTING|ZHANG ZHITAO|ZHANG SHUANGLIN|YANG SHUQUAN|MA PEIYONG (CN121107390)|DIAO RUI|HU XU|LI BOWEN|YANG CUNZHANG|QI FENGLEI|LIU XIAOHAO|CHA ZHENTING|ZHANG ZHITAO|ZHANG SHUANGLIN|YANG SHUQUAN|MA PEIYONG (CN121107390)|WANG ZHOUXIN;Hefei Hongshanxin Intellectual Property Agency (General Partnership)|Reg. Nb: 00435 (CN121107390)|The free moisture prevents the diffusion of gaseous CO2 in the cement matrix, but may also provide the necessary water reaction conditions for the relevant reactions.|In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples.|These chemical bonds may combine with some mechanical interlocking and hydrogen bonding between the phases and some coulombic interactions that result in less carbon loss of the biochar during pyrolysis.| (CN121107390)|1. The preparation method of the carbon-sealed biochar is characterized by comprising the following steps of: adding the crushed biomass to a carbon fixing agent solution to obtain a first mixture, wherein the carbon fixing agent comprises phosphoric acid and/or ferric oxide; Drying and grinding the first mixture to obtain a powdery second mixture; And pyrolyzing the second mixture under the inert gas atmosphere to obtain the carbon-sealed biochar. | (CN121107390)|The invention discloses carbon-sealed biochar and a preparation method thereof, wherein the method comprises the steps of adding crushed biomass into a carbon fixing agent solution to obtain a first mixture, wherein the carbon fixing agent comprises phosphoric acid and/or ferric oxide; and carrying out pyrolysis on the second mixture in an inert gas atmosphere to obtain the carbon-sealed biochar.|The invention relates to the field of biomass charcoal production, in particular to a biomass-based carbon dioxide adsorbent.|Therefore, the invention provides a preparation method of the carbon-sealed biochar.| (CN121107390)|CARBON SEALED BIOCHAR(100,10)|CRUSHED BIOMASS(84,3)|COULOMB IC INTERACTION(82,1)|GASEOUS CO2 DIFFUSION(72,1)|ADDING CRUSHED BIOMASS(65,2)|BIOCHAR BIOMINERALIZATION CAPACITY(65,2)|BIOMASS CARBON DIOXIDE ADSORBENT(59,1)|BIOCHAR CARBON LOSS(52,1)|CEMENT MATRIX(51,1)|GASEOUS CO2(47,1)|INERT GAS ATMOSPHERE(41,8)|PRODUCING CARBON ENCAPSULATED BIOCHAR(40,2)|PYROLYSIS(37,24)|ADSORBING CARBON DIOXIDE(37,1)|RELEVANT REACTION(37,1)|BIOMASS PYROLYSIS PRIMARY PRODUCT(33,4)|CEMENT SLURRY(32,7)|FERRIC OXIDE(30,32)|PHOSPHORIC ACID COPYROLYSIS(27,6)|CARBON FIXING AGENT SOLUTION(27,4)|PHOSPHORIC ACID(25,51)|OXIDATION RESISTANCE(23,2)|TARGET PYROLYSIS TEMPERATURE(23,2)|MECHANICAL INTERLOCKING(22,1)|PHYLLOSTACHYS PUBESCENS PYROLYSIS(21,3)|CARBON MATRIX(21,2)|CARBON FIXING(20,18)|CARBON MODIFICATION(20,1)|PRODUCING CARBON SEALED BIOCHAR(20,1)|HYDROGEN BONDING(19,1)|CARBON LOSS(18,6)|BIOMASS FIELD(18,1)|EXPERIMENTAL CARBON FIXATION(16,4)|IMPREGNATING MOSO BAMBOO(15,2)|AGENT EXPERIMENTAL YIELD(13,4)|BIOCHAR SURFACE(13,4)|HYDRATION REACTION(13,4)|MIXED MASS RATIO(13,4)|BIOCHAR INFLUENCE(13,2)|FERRIC PHOSPHATE COPYROLYSIS(13,2)|OVEN(13,2)|BIOCHAR SEQUESTRATION(13,1)|BIOCHAR YIELD(12,5)|PREPARED BIOCHAR(12,5)|CHEMICAL BOND(12,2)|BIOCHAR DIFFRACTION PEAK INTENSITY(12,1)|MOSO BAMBOO PYROLYSIS(12,1)|HEATING RATE(11,2)|BIOCHAR FOURIER INFRARED SPECTRUM(11,1)|BIOMASS COPYROLYSIS(11,1)|COPYROLYSIS CHARCOAL(11,1)|MOSO BAMBOO BIOCHAR(11,1)|MOSO BAMBOO IMPREGNATION(11,1)|WATER REACTION CONDITION(11,1)|PHYSICAL BARRIER(10,2)|IRON OXIDE(9,27)|CO PYROLYZED BIOCHAR(9,2)|MIXING MASS RATIO(9,2)|OIL BATH(9,2)|SYMMETRICAL PHOSPHATE(9,2)|BIOCHAR EXISTENCE(9,1)|BIOCHAR FLOATING(9,1)|BIOCHAR INFRARED SPECTRA(9,1)|BIOCHAR PEAK INTENSITY(9,1)|COPYROLYSIS INFLUENCE(9,1)|PROPORTION COPYROLYSIS(9,1)|PYROLYZED SOLID PRODUCT(8,4)|BIOCHAR IMPACT(8,1)|BIOCHAR MIXING(8,1)|CARBON SEQUESTRANT(8,1)|CEMENT COUPON(8,1)|CEMENT MORTAR(8,1)|CONCH COMPANY(8,1)|CONCRETE CEMENT(8,1)|FORESTRY WASTE(8,1)|PYROLYSIS EXPERIMENT(8,1)|SPECTRAL PEAK WAVELENGTH(8,1)|BIOCHAR CARBON RETENTION RATE(7,3)|COPYROLYSIS PRODUCT(7,2)|CROSSLINKING REACTION(7,2)|POSITIONAL RELATIONSHIP(7,2)|CARBON FIXATION RATE(6,5)|CARBON SEQUESTRATION RATE(6,5)|COKE(6,4)|BIOCHAR CARBON FIXING CAPABILITY(6,1)|BIOCHAR CARBON STABILITY(6,1)|BIOMASS REACTION(6,1)|CELLULOSE PHOSPHATE(6,1)|COPYROLYSIS REACTION(6,1)|DEHYDROGENIZATION REACTION(6,1)|DEMOLDED SAMPLE(6,1)|FE3O STANDARD CARD(6,1)|HYDROXYL VIBRATION(6,1)|METHANE ISOTHERMAL CHAMBER GAS(6,1)|PLANT BIOMASS(6,1)|PYROLYSIS LAST(6,1)|STABLE CARBON MORPHOLOGY(6,1)|NITROGEN FLOW(5,4)|ADDITIVE(5,3)|HEAT CONSUMPTION(5,2)|PRETREATMENT(5,2)|ANAEROBIC CONDITION(5,1)|BIOMASS ENERGY RENEWABLE NATURE(5,1)|CHARCOAL YIELD(5,1)|COMPRESSIVE STRENGTH TESTER(5,1)|EXPERIMENT CONTENT(5,1)|FE REACTION(5,1)|FERROPHOSPHORUS(5,1)|HEATING BIOMASS(5,1)|MOSO BAMBOO MECHANICAL PROPERTY(5,1)|ORGANIC FRAMEWORK(5,1)|OXIDATION CHAMBER(5,1)|PEAK INTENSITY REDUCTION(5,1)|PHOSPHORIC ACID HYDRATION(5,1)|PYROLYSIS PROCESS PYROLYSIS BEHAVIOR(5,1)|SEQUESTERING CARBON DIOXIDE(5,1)|BIOMASS PYROLYSIS(4,4)|ALDEHYDE(4,1)|AMINE COMPOUND(4,1)|AROMATICITY(4,1)|AROMATIZATION DEGREE(4,1)|ATMOSPHERIC CARBON(4,1)|CARBON FIXING PYROLYSIS(4,1)|CARBON SEALING(4,1)|CARBONIZATION CHANGE(4,1)|CEMENT TEST COMPRESSIVE STRENGTH(4,1)|CURING ROOM(4,1)|DEHYDRATION(4,1)|DEHYDROGENIZE(4,1)| (CN121107390)|1. The preparation method of the carbon-sealed biochar is characterized by comprising the following steps of:| adding the crushed biomass to a carbon fixing agent solution to obtain a first mixture, wherein the carbon fixing agent comprises phosphoric acid and/or ferric oxide; | Drying and grinding the first mixture to obtain a powdery second mixture; | And pyrolyzing the second mixture under the inert gas atmosphere to obtain the carbon-sealed biochar. |2. The method for preparing carbon-encapsulated biochar according to claim 1, wherein the biomass is phyllostachys pubescens.|3. The method for preparing carbon-encapsulated biochar according to claim 1 or 2, wherein after the crushed biomass is added to the charcoal fixing agent solution, the biomass is immersed in an oil bath at 45 ℃ and stirred for 12H, and the mixture is dried for 48H in an oven at 70 ℃.|4. The method for preparing carbon-encapsulated biochar according to claim 1, wherein the temperature range of pyrolysis of the second mixture in an inert gas atmosphere is 300-700 ℃.|5. The method for producing a carbon-encapsulated biochar according to claim 4, wherein the temperature at which the second mixture is pyrolyzed under an inert gas atmosphere is 500 ℃.|6. The method for producing a carbon-sealed biochar according to claim 1 or 5, wherein the second mixture is pyrolyzed under an inert gas atmosphere, and the temperature is raised to a target pyrolysis temperature at a heating rate of 10 ℃ per minute for 60 minutes.|7. The method for preparing carbon-sealed biochar according to claim 1, wherein in the first mixture, the mixing mass ratio of phosphoric acid to biomass is in a range of 0.5:9-5:9, and the mixing mass ratio of ferric oxide to biomass is in a range of 0.5:9-5:9.|8. The method for producing carbon-encapsulated biochar according to claim 1 or 7, wherein the mixing mass ratio of the phosphoric acid, the iron oxide and the biomass in the first mixture is 3:3:9.|9. A carbon-encapsulated biochar characterized in that the carbon-encapsulated biochar prepared by the method for preparing the carbon-encapsulated biochar according to any one of claims 1 to 8. (CN121107390)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the field of biomass charcoal production, in particular to a biomass-based carbon dioxide adsorbent.|BACKGROUND ART|[0002] The biological carbon sealing technology is paid attention to because of the renewable characteristics, agricultural and forestry waste is converted into a stable carbon form through low-temperature pyrolysis, and the remarkable benefit of 20% of the net recovery rate of atmospheric carbon can be realized. The renewable nature of biomass energy has attracted considerable attention and biochar sequestration technology is widely recognized as an effective method of sequestering carbon dioxide. However, biomass is not treated and buried, etc., biological decomposition occurs, and more carbon enters the atmosphere system, because carbon elements exist mainly in the form of cellulose, hemicellulose and lignin in plant biomass, and they are easily converted into carbon dioxide and methane isothermal chamber gas in natural environment by microorganisms. If the biochar is formed by heating biomass under anaerobic conditions (a process known as low temperature pyrolysis), the free carbon can be further converted to stable carbon, thereby achieving carbon sequestration. Because carbon undergoes decomposition, polymerization and carbonization changes during pyrolysis, it eventually converts to an aromatic and highly polymerized carbon structure, which remains in the biochar to form a relatively stable carbon morphology. And the biochar is added into the cement, so that the situation of win-win of cement performance improvement and carbon sealing can be realized.|[0003] However, the traditional pyrolysis process only can keep half of carbon in the biochar, so that it is important to find a method for efficiently fixing carbon by using the biochar.|DISCLOSURE|Disclosure of Invention|[0004] The present invention aims to solve at least one of the technical problems existing in the prior art. Therefore, the invention provides a preparation method of the carbon-sealed biochar.|[0005] The preparation method of the carbon-sealed biochar comprises the following steps of;| adding crushed biomass into a carbon fixing agent solution to obtain a first mixture, wherein the carbon fixing agent comprises phosphoric acid and/or ferric oxide, wherein the biomass can be made of moso bamboo, soaking the crushed biomass into the carbon fixing agent solution in a 45 ℃ oil bath, stirring for 12H, and drying the mixture in a 70 ℃ oven for 48H, wherein the mixing mass ratio of the phosphoric acid in the carbon fixing agent to the biomass is in the range of 0.5:9-5:9, and the mixing mass ratio of the ferric oxide to the biomass is in the range of 0.5:9-5:9. |[0006] Preferably, the mixing mass ratio of the phosphoric acid, the ferric oxide and the biomass is 3:3:9.|[0007] Step two, drying and grinding the first mixture to obtain a powdery second mixture;| And thirdly, pyrolyzing the second mixture in an inert gas atmosphere to obtain the carbon-sealed biochar, wherein the temperature range of the pyrolysis of the second mixture in the inert gas atmosphere is 300-700 ℃, preferably, when the second mixture is pyrolyzed in the inert gas atmosphere, the temperature is firstly increased to a target pyrolysis temperature at a heating rate of 10 ℃ per minute, and the pyrolysis lasts for 60 minutes, and the target temperature is 500 ℃. |[0008] Wherein, compared with the biochar prepared without adding salt, the H/C ratio in the biochar prepared with adding salt is lower, which shows that the C aromaticity is higher, and the higher the H/C contained in the biochar is, the lower the stability is. And the addition of the carbon fixing agent causes more dehydrogenation reaction to occur in the pyrolysis process, so that the carbonization and aromatization degree is increased, and the carbon stability of the biochar is enhanced.|[0009] Hydration of phosphoric acid can deoxidize and dehydrogenate to promote dehydration. The addition of Fe2O3 and the synergistic effect of the prepared biochar have obviously increased O element, which is the effect of chemical bonds between carboxyl and hydroxyl groups on the surface of the biochar and iron particle phases, and the existence of the biochar has obviously increased O element. These chemical bonds may combine with some mechanical interlocking and hydrogen bonding between the phases and some coulombic interactions that result in less carbon loss of the biochar during pyrolysis.|[0010] The carbon-sealed biochar prepared by the preparation method of the carbon-sealed biochar is provided. The carbon sequestration rate of the biochar prepared by the preparation method can reach 78 percent, and is beneficial to the carbon sequestration rate of biomass.|[0011] Advantageous effects|[0012] The invention prepares the biochar with high yield and high carbon content by co-pyrolysis of phosphoric acid, ferric oxide and biomass, improves the carbon fixation rate of the biochar by utilizing the synergistic effect of the phosphoric acid and the ferric oxide, forms a physical barrier on the surface of the biochar, enhances the oxidation resistance and biomineralization capacity of the biochar, and limits the escape of biomass pyrolysis primary products, thereby leading the biomass pyrolysis primary products to be retained in a carbon matrix, and leading more carbon to be reserved and high yield. The modified carbon dioxide is applied to cement slurry, and the hydration reaction of cement is stimulated to improve the mechanical property by utilizing all phosphorus and iron elements contained in biochar|After the biochar prepared by co-pyrolysis of phosphoric acid, ferric oxide and moso bamboo is added into the concrete cement, the mechanical property is improved, 40.8KN is achieved in 7 days, and 55.8KN is achieved in 28 days. In this way, the hydration reaction in the cement slurry is stimulated by the combined action of the added phosphoric acid and ferric oxide, and the excellent pore structure in the prepared biochar is added, so that the mechanical property of the cement is greatly improved.|DRAWINGS DESCRIPTION|[0013] The foregoing and/or additional aspects and advantages of the invention will become apparent and may be better understood from the following description of embodiments taken in conjunction with the accompanying drawings in which:| FIG. 1 is a graph showing the impact of biochar prepared by doping different carbon fixing agents on the compressive properties of cement coupons according to an embodiment of the present invention; | FIG. 2 is an X-ray diffraction pattern of a co-pyrolysis product according to embodiments of the present invention; | FIG. 3 is a Fourier infrared spectrum of biochar prepared from different carbon fixing agents according to an embodiment of the present invention. |INVENTION MODE|Detailed Description|[0014] Embodiments of the present invention are described in detail below.|[0015] The quality of the solid product (biochar) after pyrolysis is calculated according to the quality difference (M0=M1-M2) before and after the reaction vessel, the actual yield Y= (M0/M3) of the solid product is 100%, the quality of the solid added into pyrolysis is M3, and the carbon element content is obtained according to the element analysis result.|[0016] The yields of solid products from separate pyrolysis of biomass and phosphoric acid or iron oxide under the same pyrolysis conditions are denoted Y1 and Y2, respectively, and the theoretical yields of co-pyrolysis of biomass and phosphoric acid and iron oxide are calculated from the mass ratio of the addition of the mixture, i.e. Ytheory =w1y1+w2y2 (W1 and W2 are the mass ratios of phosphoric acid and iron oxide, respectively).|[0017] The carbon sequestration rate is calculated as the mass ratio of carbon elements before and after pyrolysis, i.e., cr= (Cbr/Cbs) x y x 100%, cbr is the carbon content of the solids after pyrolysis, cbs is the carbon content of the solids before pyrolysis, i.e., cbs=cbr1 x 1 (1-Wa), wa is the ratio of the total amount of the carbon sequestrants in the solid mass, the carbon sequestration rate after the co-pyrolysis reaction is calculated as the experimental carbon sequestration rate, the theoretical carbon sequestration rate obtained by pyrolysis of biomass and phosphoric acid or iron oxide alone (assuming phosphoric acid and iron oxide do not react, no synergistic operation occurs), and the carbon sequestration rate obtained by pyrolysis of biomass and phosphoric acid or iron oxide alone under the same pyrolysis conditions according to formula CRtheory =w1cr1+w2cr2 (C1 and C2, respectively). And subsequently adjusting the proportion of phosphoric acid to ferric oxide, performing a pyrolysis experiment, and comparing the yield and the carbon fixation rate of the biochar.|[0018] Adding the prepared biochar into cement slurry, placing the prepared cement test block in a curing room, curing for a selected time, and testing the compressive strength of the cement test block by using a press machine to compare the influence of different biochars on the cement performance.|[0019] Example 1|In the embodiment, the influence of the co-pyrolysis of different carbon fixing agents and biomass and the synergistic effect of ferrophosphorus on the yield and carbon fixing rate of the biochar is studied, namely, the biochar is prepared by respectively adopting phosphoric acid, ferric oxide, phosphoric acid and ferric oxide (1:1) and the co-pyrolysis of ferric phosphate and biomass, and the specific steps are as follows:| The biomass and the carbon fixing agent are mixed according to the ratio of 9:1, the biomass and the carbon fixing agent are impregnated, the dried mixture is ground uniformly and then pyrolyzed under the pyrolysis conditions of 500 ℃ pyrolysis temperature, 60 min residence time, 200 mL/min nitrogen flow and the like, and the yield and the experimental and theoretical content of the carbon fixing rate of the pyrolyzed solid product are calculated according to the mode. The results are shown in Table 1: | TABLE 1 influence of different carbon fixing agents on biochar yield and carbon fixing rate by co-pyrolysis with biomass |Carbon fixing agentExperimental yield%Experimental carbon fixation%Is not added with25.9746.73Phosphoric acid40.0070.92Iron oxide31.8947.79Iron phosphate32.3851.15Phosphoric acid @ iron oxide43.2965.64|TABLE 2 influence of synergistic effects of phosphoric acid and iron oxide on biochar yield and carbon fixation|Synergistic effectYield%Carbon fixation rate%Calculated value36.3457.86Experimental values43.2965.64Value-added6.957.79|From the results shown in the table 2, the yield and the carbon fixation rate experimental values of the biochar obtained by co-pyrolysis of the phosphoric acid and the ferric oxide and the phyllostachys pubescens are both larger than theoretical values, which indicates that the phosphoric acid and the ferric oxide have the carbon fixation effect on the biomass pyrolysis for preparing the biochar.|[0020] Among these, it was found that the strong synergistic action of phosphoric acid and iron oxide increased the carbon fixation rate of biochar, probably in the pyrolysis process, H 3PO4 and Fe 2O3 reacted with biomass to form P-O-C and Fe-O-C.|[0021] Secondly, the ferric phosphate is found to have no obvious effect on increasing the yield and the carbon fixation rate of the bamboo pyrolysis biochar, and further proves that the ferric phosphate is not formed by the phosphoric acid and the ferric oxide, so that the yield and the carbon fixation rate of the biochar are improved.|[0022] Example 2|In this example, the effect of co-pyrolysis of different proportions (phosphoric acid and ferric oxide) and moso bamboo on the charcoal yield and carbon fixation rate under synergistic effect was studied, namely, the co-pyrolysis charcoal was prepared by using the mixing proportions (phosphoric acid: ferric oxide: biomass) of 1:0:9, 1:0.5:9, 1:1:9, 1:1.5:9, 1:2:9, 1:2.5:9, 1:3:9 and 1:5:9, respectively,|The method comprises the following specific steps:| impregnating moso bamboo, phosphoric acid and ferric oxide in different proportions, grinding the dried mixture uniformly, then carrying out pyrolysis under the pyrolysis conditions of 500 ℃ pyrolysis temperature, 60 min residence time, 200 mL/min nitrogen flow and the like, and calculating the yield and carbon fixation rate of the pyrolyzed solid product according to the mode. The results are shown in Table 3: | TABLE 3 influence of phosphoric acid and iron oxide in different ratios on biochar yield and carbon sequestration after Phyllostachys Pubescens pyrolysis |Carbon fixing agentExperimental yield%Experimental carbon fixation%1:0:940.0070.921:0.5:941.7968.701:1:942.7165.991:1.5:945.8172.301:2:947.7472.631:2.5:948.3375.681:3:951.7563.261:5:955.1562.58|From the results shown in Table 3 above, it can be seen that the carbon retention during pyrolysis tends to decrease first and then increase and then decrease as elemental iron increases. When the mass ratio of added phosphoric acid to iron oxide is 1:1, the carbon retention of biochar is 5% lower than that of co-pyrolysis with only phosphoric acid, probably due to the fact that small amounts of iron oxide are added to combine with PO 43- under acidic conditions to form complexes, thus impeding further reaction of Fe and P with coke. The quality of the ferric oxide is continuously increased, the carbon retention rate of the biochar is increased, and when the quality is 1:2.5, the carbon retention rate reaches the maximum value of 76 percent, because the activation energy of the surface of the biochar is reduced due to the addition of the ferric oxide, and the coke is more prone to form a more stable structure with Fe and P.|[0023] And meanwhile, compared with the co-pyrolysis by independently adding phosphoric acid, the carbon retention rate is improved by 5%, which indicates that the synergistic effect of the two improves the carbon fixing capability of the biochar in the pyrolysis process. As the content of iron oxide continues to increase, the carbon retention of biochar tends to decrease, indicating that iron oxide has begun to undergo redox reactions with coke, thereby increasing carbon loss during pyrolysis.|[0024] Example 3|In this example, the effect of different amounts of phosphoric acid and iron oxide (ensuring the ratio of phosphoric acid to iron oxide is 1:1) on the yield and carbon fixation rate of the co-pyrolyzed biochar of moso bamboos and carbon fixation agents was studied, namely, the co-pyrolyzed biochar was prepared by adopting the mixing ratios of 0:0:9, 0.5:0.5:9, 1:1:9, 1.5:1.5:9, 2:2:9, 2.5:2.5:9, 3:3:9 and 5:5:9 (phosphoric acid: iron oxide: biomass), respectively, and the specific steps are as follows:| Impregnating moso bamboos with phosphoric acid and ferric oxide in different amounts, grinding the dried mixture uniformly, then carrying out pyrolysis under the pyrolysis conditions of 500 ℃ pyrolysis temperature, 60 min residence time, 200 mL/min nitrogen flow and the like, and calculating the yield and carbon fixation rate of the pyrolyzed solid product according to the mode. |[0025] The results are shown in Table 4:| TABLE 4 influence of different amounts of phosphoric acid and iron oxide on biochar yield and carbon sequestration after Phyllostachys Pubescens pyrolysis |Carbon fixing agentExperimental yield%Experimental carbon fixation%0:0:925.9746.730.5:0.5:938.5963.631:1:942.7165.991.5:1.5:947.3272.122:2:949.2472.452.5:2.5:951.5174.473:3:955.1178.475:5:960.4745.49|From the results shown in Table 4 above, it can be seen that the carbon retention of biochar is greatly improved when a small amount of phosphoric acid and iron oxide are added, and the carbon retention is improved by 17% compared with the pyrolysis of moso bamboo alone, and the synergistic effect of phosphoric acid and iron oxide on the reduction of carbon loss in the pyrolysis process is also shown. As additives increase, so does the carbon retention, which reaches 78% maximum.|[0026] Thus, in this way, carbon loss during pyrolysis can be reduced and more carbon is immobilized in the biochar at high char yields. Of course, the additive is not as good as the excessive amount, and the excessive addition of salt can reduce the carbon retention rate of the biochar, and the proper proportion and the proper dosage are favorable for guiding the production of the biochar and reducing the carbon loss in the pyrolysis process. The optimum dosage ratio is 3:3:9, and this amount can be selected as a guideline for production.|[0027] Example 4|In the embodiment, the influence of different temperatures (ensuring that the ratio of phosphoric acid to ferric oxide is 1:1) on the yield and the carbon fixation rate of the co-pyrolyzed biochar of the moso bamboos and the carbon fixation agent is studied, namely, the co-pyrolyzed biochar is prepared at the temperatures of 300 ℃, 400 ℃,500 ℃, 600 ℃ and 700 ℃ respectively, and the specific steps are as follows:| Impregnating moso bamboos, phosphoric acid with different dosages and ferric oxide, uniformly grinding the dried mixture, performing pyrolysis under the pyrolysis conditions of 60 min residence time, 200 mL/min nitrogen flow and the like at different pyrolysis temperatures, and calculating the yield and the carbon fixation rate of the pyrolyzed solid product according to the mode. The results are shown in Table 5: | TABLE 5 influence of phosphoric acid and iron oxide in different ratios on biochar yield and carbon sequestration after Phyllostachys Pubescens pyrolysis |Carbon fixing agentExperimental yield%Experimental carbon fixation%300°C51.8568.85400°C48.4267.43500°C47.6572.25600°C44.8768.85700°C44.3069.18|From the results shown in Table 5 above, it can be seen that the carbon retention during pyrolysis tends to increase and decrease with increasing temperature. The carbon retention rate of the biochar is highest and is 72.25% at the temperature of 500 ℃, which is a method for preparing low-carbon fuel by low-temperature carbon-fixing pyrolysis. At temperatures below 500 ℃, the heat consumption is low, but the carbon fixation rate is low, which is unfavorable for the production of low-carbon fuels, while at temperatures above 500 ℃, the heat consumption is high and the carbon fixation rate is not increased.|[0028] Thus 500 ℃ is the most suitable temperature for the preparation of biochar. This is probably due to the fact that the iron oxide and phosphoric acid added at this temperature combine better with carbon to form a stable structure, so that more carbon element remains in the biochar, thereby improving the carbon fixation rate.|[0029] Viewing example 1|In this example, the influence of different biochars on cement slurries was studied, namely, additive-free moso bamboo biochar, moso bamboo biochar added with phosphoric acid, moso bamboo biochar added with ferric oxide, and moso bamboo biochar added with phosphoric acid and ferric oxide were respectively added to cement slurries, and cement-modified compressive property test was performed.|[0030] Specifically, the cement is P.O.42.5 cement from the conch company of Anhui province, the water cement ratio is 0.4, and the biochar mixing amount is 3wt%. Sample codes are as in Table S1, wherein the preparation procedure is described by way of example only in the 1:2.5:9 ratio.|[0031] The dry material and biochar were mixed in a stirrer at low speed 140 rpm for 3 min followed by high speed mixing at 280rpm for 1min, then mixing water was added, then mixed at low speed 3 min, and mixed at high speed at 280rpm for 3 min. After the mixing is completed, pouring the fresh mixture into a mould with the size of 40mm multiplied by 40mm multiplied by 40mm, vibrating the mould on a vibrating table for 10 times to avoid the biochar floating on the upper layer of the test block, and fully stirring the slurry by using a stirring rod to release bubbles from the slurry so as to ensure the stability of the test of the sample.|[0032] These samples were subjected to in-mold pretreatment for 24 hours and then to a release treatment. The temperature and Relative Humidity (RH) of the pretreatment were 20℃and 95%, respectively. The purpose of the pretreatment is to remove excess free water from the sample. The free moisture prevents the diffusion of gaseous CO2 in the cement matrix, but may also provide the necessary water reaction conditions for the relevant reactions. The demolded sample is placed in an oxidation chamber and cured to a selected test time. The compressive strength of the cement mortar is measured by adopting a STYE-300C compressive strength tester, and the loading rate is 1.4 kN/s. Each set of experiments was run three times and the average was determined as the final result. After curing for 7 days and 28 days, the compressive properties of the corresponding cement test blocks were tested.|[0033] As shown in the results of FIG. 1, the mechanical properties of the moso bamboo added with no additive are improved to a certain extent, the mechanical properties are obviously improved after the iron oxide or the biochar prepared by the co-pyrolysis of the phosphoric acid and the moso bamboo is added, the mechanical properties are highest after the biochar prepared by the co-pyrolysis of the phosphoric acid and the iron oxide and the moso bamboo is added, and the mechanical properties reach 40.8KN in 7 days and 55.8KN in 28 days.|[0034] The added phosphoric acid and ferric oxide act together to stimulate hydration reaction in the cement slurry, and the excellent pore structure in the prepared biochar is added, so that the mechanical property of cement is greatly improved.|[0035] Furthermore, as can be seen from the X-ray diffraction pattern of the co-pyrolysis product of fig. 2, since the carbon material under the pyrolysis is of an amorphous structure, all diffraction peaks can be attributed to the decomposition products of Fe and P. In the biochar added with Fe2O3, the diffraction peak is consistent with the standard card of Fe3O4, which is consistent with the product distribution and pyrolysis behavior of the pyrolysis process, and further indicates that Fe2O3 has little influence on the carbon retention rate under the pyrolysis of low temperature.|[0036] While a diffraction peak of the biochar prepared by adding phosphoric acid is observed at a position of 21 degrees 2 theta, a large broad peak is corresponding to 002 strips of a graphite structure, and the result of the broad peak shows that the biochar prepared by phosphoric acid is of an amorphous structure.|[0037] The diffraction peak intensity of the biochar prepared under the synergistic effect is obviously reduced, compared with the biochar prepared by adding ferric oxide, the peak intensity reduction and the disappearance of one diffraction peak are observed at the position of 36 degrees of 2 theta, which indicates that the oxidation-reduction reaction of iron and coke is slowed down in the pyrolysis process, and further proves that the synergistic effect of phosphoric acid and ferric oxide can reduce the carbon loss in the pyrolysis process.|[0038] The diffraction peaks of the biochar prepared by co-pyrolysis of the ferric phosphate and the moso bamboo are completely different, and further prove that the ferric phosphate and the ferric oxide do not generate double decomposition reaction to generate the ferric phosphate.|[0039] As can be seen from the Fourier infrared spectra of the different biochars shown in FIG. 3, the broad peaks observed at (3200-3700 cm-1) of the prepared biochars are characteristic of stretching vibration of hydroxyl (-OH) groups in hydrogen bonds from carboxyl groups, phenol or alcohol and water. In some cases it may also correspond to N-H stretching vibrations in the amino compound. The peaks observed at (2800-3000 cm-1) may indicate the presence of saturated symmetrical and asymmetrical aliphatic C-H stretching vibrations. The two peaks at 1594 and 1624 can be attributed to the stretching vibration of c=c, c=o in ketones, quinones, aldehydes, lactones and ketones. The peak in the spectral region between 1150cm-1 and 950cm-1 is attributed to the functional group formed by phosphate and biochar. Biochar prepared using phosphoric acid and ferric phosphate is attributable to symmetrical phosphate (PO 2-) stretching at 1089cm-1, i.e., stretching vibration of the phosphate groups. Since the spectral peak wavelength of P-O-C is shorter than that of the symmetrical phosphate (PO 2-) and is attributable to P-O-C at 1025cm-1 and 943cm-1, a distinct band was observed for biochar prepared by treatment with phosphoric acid and synergy.|[0040] The crosslinking reaction is the primary mechanism to retain C in the solid phase, and this result suggests that the reaction of biomass with H3PO4 may lead to the formation of cellulose phosphate, and the possible presence of C-O-PO3 type groups (i.e., (CO) 3PO, (CO) 2 PO2 and (CO) PO 3) may physically protect the C structure, thereby reducing C losses that do not occur with biochar produced from ferric phosphate.|[0041] At 560cm-1, which is attributable to Fe-O-C, this crosslinking reaction is effective in retaining C in the char. Meanwhile, the previous research results show that Fe ions can interact with oxygen-containing groups in the organic framework and then be converted into inorganic oxides.|[0042] This result indicates that fe—o complexes or iron oxides may be present on the surface. The peak intensity of the biochar prepared under the synergistic effect of 1025cm < -1 > and 943cm < -1 > is higher, namely the content of P-O-C is increased, and the added Fe possibly catalyzes the reaction of P, so that more P-O-C is obtained in the biochar to wrap more C, and more carbon is sealed in the biochar.|[0043] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.|[0044] In the description of the present specification, reference to the terms "one embodiment," "some embodiments," "illustrative embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples.|[0045] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the spirit and scope of the invention as defined by the appended claims and their equivalents. (CN121107390)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the field of biomass charcoal production, in particular to a biomass-based carbon dioxide adsorbent.|BACKGROUND ART|[0002] The biological carbon sealing technology is paid attention to because of the renewable characteristics, agricultural and forestry waste is converted into a stable carbon form through low-temperature pyrolysis, and the remarkable benefit of 20% of the net recovery rate of atmospheric carbon can be realized. The renewable nature of biomass energy has attracted considerable attention and biochar sequestration technology is widely recognized as an effective method of sequestering carbon dioxide. However, biomass is not treated and buried, etc., biological decomposition occurs, and more carbon enters the atmosphere system, because carbon elements exist mainly in the form of cellulose, hemicellulose and lignin in plant biomass, and they are easily converted into carbon dioxide and methane isothermal chamber gas in natural environment by microorganisms. If the biochar is formed by heating biomass under anaerobic conditions (a process known as low temperature pyrolysis), the free carbon can be further converted to stable carbon, thereby achieving carbon sequestration. Because carbon undergoes decomposition, polymerization and carbonization changes during pyrolysis, it eventually converts to an aromatic and highly polymerized carbon structure, which remains in the biochar to form a relatively stable carbon morphology. And the biochar is added into the cement, so that the situation of win-win of cement performance improvement and carbon sealing can be realized.|[0003] However, the traditional pyrolysis process only can keep half of carbon in the biochar, so that it is important to find a method for efficiently fixing carbon by using the biochar.|DISCLOSURE|Disclosure of Invention|[0004] The present invention aims to solve at least one of the technical problems existing in the prior art. Therefore, the invention provides a preparation method of the carbon-sealed biochar.|[0005] The preparation method of the carbon-sealed biochar comprises the following steps of;| adding crushed biomass into a carbon fixing agent solution to obtain a first mixture, wherein the carbon fixing agent comprises phosphoric acid and/or ferric oxide, wherein the biomass can be made of moso bamboo, soaking the crushed biomass into the carbon fixing agent solution in a 45 ℃ oil bath, stirring for 12H, and drying the mixture in a 70 ℃ oven for 48H, wherein the mixing mass ratio of the phosphoric acid in the carbon fixing agent to the biomass is in the range of 0.5:9-5:9, and the mixing mass ratio of the ferric oxide to the biomass is in the range of 0.5:9-5:9. |[0006] Preferably, the mixing mass ratio of the phosphoric acid, the ferric oxide and the biomass is 3:3:9.|[0007] Step two, drying and grinding the first mixture to obtain a powdery second mixture;| And thirdly, pyrolyzing the second mixture in an inert gas atmosphere to obtain the carbon-sealed biochar, wherein the temperature range of the pyrolysis of the second mixture in the inert gas atmosphere is 300-700 ℃, preferably, when the second mixture is pyrolyzed in the inert gas atmosphere, the temperature is firstly increased to a target pyrolysis temperature at a heating rate of 10 ℃ per minute, and the pyrolysis lasts for 60 minutes, and the target temperature is 500 ℃. |[0008] Wherein, compared with the biochar prepared without adding salt, the H/C ratio in the biochar prepared with adding salt is lower, which shows that the C aromaticity is higher, and the higher the H/C contained in the biochar is, the lower the stability is. And the addition of the carbon fixing agent causes more dehydrogenation reaction to occur in the pyrolysis process, so that the carbonization and aromatization degree is increased, and the carbon stability of the biochar is enhanced.|[0009] Hydration of phosphoric acid can deoxidize and dehydrogenate to promote dehydration. The addition of Fe2O3 and the synergistic effect of the prepared biochar have obviously increased O element, which is the effect of chemical bonds between carboxyl and hydroxyl groups on the surface of the biochar and iron particle phases, and the existence of the biochar has obviously increased O element. These chemical bonds may combine with some mechanical interlocking and hydrogen bonding between the phases and some coulombic interactions that result in less carbon loss of the biochar during pyrolysis.|[0010] The carbon-sealed biochar prepared by the preparation method of the carbon-sealed biochar is provided. The carbon sequestration rate of the biochar prepared by the preparation method can reach 78 percent, and is beneficial to the carbon sequestration rate of biomass.|[0011] Advantageous effects|[0012] The invention prepares the biochar with high yield and high carbon content by co-pyrolysis of phosphoric acid, ferric oxide and biomass, improves the carbon fixation rate of the biochar by utilizing the synergistic effect of the phosphoric acid and the ferric oxide, forms a physical barrier on the surface of the biochar, enhances the oxidation resistance and biomineralization capacity of the biochar, and limits the escape of biomass pyrolysis primary products, thereby leading the biomass pyrolysis primary products to be retained in a carbon matrix, and leading more carbon to be reserved and high yield. The modified carbon dioxide is applied to cement slurry, and the hydration reaction of cement is stimulated to improve the mechanical property by utilizing all phosphorus and iron elements contained in biochar|After the biochar prepared by co-pyrolysis of phosphoric acid, ferric oxide and moso bamboo is added into the concrete cement, the mechanical property is improved, 40.8KN is achieved in 7 days, and 55.8KN is achieved in 28 days. In this way, the hydration reaction in the cement slurry is stimulated by the combined action of the added phosphoric acid and ferric oxide, and the excellent pore structure in the prepared biochar is added, so that the mechanical property of the cement is greatly improved.|DRAWINGS DESCRIPTION|[0013] The foregoing and/or additional aspects and advantages of the invention will become apparent and may be better understood from the following description of embodiments taken in conjunction with the accompanying drawings in which:| FIG. 1 is a graph showing the impact of biochar prepared by doping different carbon fixing agents on the compressive properties of cement coupons according to an embodiment of the present invention; | FIG. 2 is an X-ray diffraction pattern of a co-pyrolysis product according to embodiments of the present invention; | FIG. 3 is a Fourier infrared spectrum of biochar prepared from different carbon fixing agents according to an embodiment of the present invention. |INVENTION MODE|Detailed Description|[0014] Embodiments of the present invention are described in detail below.|[0015] The quality of the solid product (biochar) after pyrolysis is calculated according to the quality difference (M0=M1-M2) before and after the reaction vessel, the actual yield Y= (M0/M3) of the solid product is 100%, the quality of the solid added into pyrolysis is M3, and the carbon element content is obtained according to the element analysis result.|[0016] The yields of solid products from separate pyrolysis of biomass and phosphoric acid or iron oxide under the same pyrolysis conditions are denoted Y1 and Y2, respectively, and the theoretical yields of co-pyrolysis of biomass and phosphoric acid and iron oxide are calculated from the mass ratio of the addition of the mixture, i.e. Ytheory =w1y1+w2y2 (W1 and W2 are the mass ratios of phosphoric acid and iron oxide, respectively).|[0017] The carbon sequestration rate is calculated as the mass ratio of carbon elements before and after pyrolysis, i.e., cr= (Cbr/Cbs) x y x 100%, cbr is the carbon content of the solids after pyrolysis, cbs is the carbon content of the solids before pyrolysis, i.e., cbs=cbr1 x 1 (1-Wa), wa is the ratio of the total amount of the carbon sequestrants in the solid mass, the carbon sequestration rate after the co-pyrolysis reaction is calculated as the experimental carbon sequestration rate, the theoretical carbon sequestration rate obtained by pyrolysis of biomass and phosphoric acid or iron oxide alone (assuming phosphoric acid and iron oxide do not react, no synergistic operation occurs), and the carbon sequestration rate obtained by pyrolysis of biomass and phosphoric acid or iron oxide alone under the same pyrolysis conditions according to formula CRtheory =w1cr1+w2cr2 (C1 and C2, respectively). And subsequently adjusting the proportion of phosphoric acid to ferric oxide, performing a pyrolysis experiment, and comparing the yield and the carbon fixation rate of the biochar.|[0018] Adding the prepared biochar into cement slurry, placing the prepared cement test block in a curing room, curing for a selected time, and testing the compressive strength of the cement test block by using a press machine to compare the influence of different biochars on the cement performance.|[0019] Example 1|In the embodiment, the influence of the co-pyrolysis of different carbon fixing agents and biomass and the synergistic effect of ferrophosphorus on the yield and carbon fixing rate of the biochar is studied, namely, the biochar is prepared by respectively adopting phosphoric acid, ferric oxide, phosphoric acid and ferric oxide (1:1) and the co-pyrolysis of ferric phosphate and biomass, and the specific steps are as follows:| The biomass and the carbon fixing agent are mixed according to the ratio of 9:1, the biomass and the carbon fixing agent are impregnated, the dried mixture is ground uniformly and then pyrolyzed under the pyrolysis conditions of 500 ℃ pyrolysis temperature, 60 min residence time, 200 mL/min nitrogen flow and the like, and the yield and the experimental and theoretical content of the carbon fixing rate of the pyrolyzed solid product are calculated according to the mode. The results are shown in Table 1: | TABLE 1 influence of different carbon fixing agents on biochar yield and carbon fixing rate by co-pyrolysis with biomass |Carbon fixing agentExperimental yield%Experimental carbon fixation%Is not added with25.9746.73Phosphoric acid40.0070.92Iron oxide31.8947.79Iron phosphate32.3851.15Phosphoric acid @ iron oxide43.2965.64|TABLE 2 influence of synergistic effects of phosphoric acid and iron oxide on biochar yield and carbon fixation|Synergistic effectYield%Carbon fixation rate%Calculated value36.3457.86Experimental values43.2965.64Value-added6.957.79|From the results shown in the table 2, the yield and the carbon fixation rate experimental values of the biochar obtained by co-pyrolysis of the phosphoric acid and the ferric oxide and the phyllostachys pubescens are both larger than theoretical values, which indicates that the phosphoric acid and the ferric oxide have the carbon fixation effect on the biomass pyrolysis for preparing the biochar.|[0020] Among these, it was found that the strong synergistic action of phosphoric acid and iron oxide increased the carbon fixation rate of biochar, probably in the pyrolysis process, H 3PO4 and Fe 2O3 reacted with biomass to form P-O-C and Fe-O-C.|[0021] Secondly, the ferric phosphate is found to have no obvious effect on increasing the yield and the carbon fixation rate of the bamboo pyrolysis biochar, and further proves that the ferric phosphate is not formed by the phosphoric acid and the ferric oxide, so that the yield and the carbon fixation rate of the biochar are improved.|[0022] Example 2|In this example, the effect of co-pyrolysis of different proportions (phosphoric acid and ferric oxide) and moso bamboo on the charcoal yield and carbon fixation rate under synergistic effect was studied, namely, the co-pyrolysis charcoal was prepared by using the mixing proportions (phosphoric acid: ferric oxide: biomass) of 1:0:9, 1:0.5:9, 1:1:9, 1:1.5:9, 1:2:9, 1:2.5:9, 1:3:9 and 1:5:9, respectively,|The method comprises the following specific steps:| impregnating moso bamboo, phosphoric acid and ferric oxide in different proportions, grinding the dried mixture uniformly, then carrying out pyrolysis under the pyrolysis conditions of 500 ℃ pyrolysis temperature, 60 min residence time, 200 mL/min nitrogen flow and the like, and calculating the yield and carbon fixation rate of the pyrolyzed solid product according to the mode. The results are shown in Table 3: | TABLE 3 influence of phosphoric acid and iron oxide in different ratios on biochar yield and carbon sequestration after Phyllostachys Pubescens pyrolysis |Carbon fixing agentExperimental yield%Experimental carbon fixation%1:0:940.0070.921:0.5:941.7968.701:1:942.7165.991:1.5:945.8172.301:2:947.7472.631:2.5:948.3375.681:3:951.7563.261:5:955.1562.58|From the results shown in Table 3 above, it can be seen that the carbon retention during pyrolysis tends to decrease first and then increase and then decrease as elemental iron increases. When the mass ratio of added phosphoric acid to iron oxide is 1:1, the carbon retention of biochar is 5% lower than that of co-pyrolysis with only phosphoric acid, probably due to the fact that small amounts of iron oxide are added to combine with PO 43- under acidic conditions to form complexes, thus impeding further reaction of Fe and P with coke. The quality of the ferric oxide is continuously increased, the carbon retention rate of the biochar is increased, and when the quality is 1:2.5, the carbon retention rate reaches the maximum value of 76 percent, because the activation energy of the surface of the biochar is reduced due to the addition of the ferric oxide, and the coke is more prone to form a more stable structure with Fe and P.|[0023] And meanwhile, compared with the co-pyrolysis by independently adding phosphoric acid, the carbon retention rate is improved by 5%, which indicates that the synergistic effect of the two improves the carbon fixing capability of the biochar in the pyrolysis process. As the content of iron oxide continues to increase, the carbon retention of biochar tends to decrease, indicating that iron oxide has begun to undergo redox reactions with coke, thereby increasing carbon loss during pyrolysis.|[0024] Example 3|In this example, the effect of different amounts of phosphoric acid and iron oxide (ensuring the ratio of phosphoric acid to iron oxide is 1:1) on the yield and carbon fixation rate of the co-pyrolyzed biochar of moso bamboos and carbon fixation agents was studied, namely, the co-pyrolyzed biochar was prepared by adopting the mixing ratios of 0:0:9, 0.5:0.5:9, 1:1:9, 1.5:1.5:9, 2:2:9, 2.5:2.5:9, 3:3:9 and 5:5:9 (phosphoric acid: iron oxide: biomass), respectively, and the specific steps are as follows:| Impregnating moso bamboos with phosphoric acid and ferric oxide in different amounts, grinding the dried mixture uniformly, then carrying out pyrolysis under the pyrolysis conditions of 500 ℃ pyrolysis temperature, 60 min residence time, 200 mL/min nitrogen flow and the like, and calculating the yield and carbon fixation rate of the pyrolyzed solid product according to the mode. |[0025] The results are shown in Table 4:| TABLE 4 influence of different amounts of phosphoric acid and iron oxide on biochar yield and carbon sequestration after Phyllostachys Pubescens pyrolysis |Carbon fixing agentExperimental yield%Experimental carbon fixation%0:0:925.9746.730.5:0.5:938.5963.631:1:942.7165.991.5:1.5:947.3272.122:2:949.2472.452.5:2.5:951.5174.473:3:955.1178.475:5:960.4745.49|From the results shown in Table 4 above, it can be seen that the carbon retention of biochar is greatly improved when a small amount of phosphoric acid and iron oxide are added, and the carbon retention is improved by 17% compared with the pyrolysis of moso bamboo alone, and the synergistic effect of phosphoric acid and iron oxide on the reduction of carbon loss in the pyrolysis process is also shown. As additives increase, so does the carbon retention, which reaches 78% maximum.|[0026] Thus, in this way, carbon loss during pyrolysis can be reduced and more carbon is immobilized in the biochar at high char yields. Of course, the additive is not as good as the excessive amount, and the excessive addition of salt can reduce the carbon retention rate of the biochar, and the proper proportion and the proper dosage are favorable for guiding the production of the biochar and reducing the carbon loss in the pyrolysis process. The optimum dosage ratio is 3:3:9, and this amount can be selected as a guideline for production.|[0027] Example 4|In the embodiment, the influence of different temperatures (ensuring that the ratio of phosphoric acid to ferric oxide is 1:1) on the yield and the carbon fixation rate of the co-pyrolyzed biochar of the moso bamboos and the carbon fixation agent is studied, namely, the co-pyrolyzed biochar is prepared at the temperatures of 300 ℃, 400 ℃,500 ℃, 600 ℃ and 700 ℃ respectively, and the specific steps are as follows:| Impregnating moso bamboos, phosphoric acid with different dosages and ferric oxide, uniformly grinding the dried mixture, performing pyrolysis under the pyrolysis conditions of 60 min residence time, 200 mL/min nitrogen flow and the like at different pyrolysis temperatures, and calculating the yield and the carbon fixation rate of the pyrolyzed solid product according to the mode. The results are shown in Table 5: | TABLE 5 influence of phosphoric acid and iron oxide in different ratios on biochar yield and carbon sequestration after Phyllostachys Pubescens pyrolysis |Carbon fixing agentExperimental yield%Experimental carbon fixation%300°C51.8568.85400°C48.4267.43500°C47.6572.25600°C44.8768.85700°C44.3069.18|From the results shown in Table 5 above, it can be seen that the carbon retention during pyrolysis tends to increase and decrease with increasing temperature. The carbon retention rate of the biochar is highest and is 72.25% at the temperature of 500 ℃, which is a method for preparing low-carbon fuel by low-temperature carbon-fixing pyrolysis. At temperatures below 500 ℃, the heat consumption is low, but the carbon fixation rate is low, which is unfavorable for the production of low-carbon fuels, while at temperatures above 500 ℃, the heat consumption is high and the carbon fixation rate is not increased.|[0028] Thus 500 ℃ is the most suitable temperature for the preparation of biochar. This is probably due to the fact that the iron oxide and phosphoric acid added at this temperature combine better with carbon to form a stable structure, so that more carbon element remains in the biochar, thereby improving the carbon fixation rate.|[0029] Viewing example 1|In this example, the influence of different biochars on cement slurries was studied, namely, additive-free moso bamboo biochar, moso bamboo biochar added with phosphoric acid, moso bamboo biochar added with ferric oxide, and moso bamboo biochar added with phosphoric acid and ferric oxide were respectively added to cement slurries, and cement-modified compressive property test was performed.|[0030] Specifically, the cement is P.O.42.5 cement from the conch company of Anhui province, the water cement ratio is 0.4, and the biochar mixing amount is 3wt%. Sample codes are as in Table S1, wherein the preparation procedure is described by way of example only in the 1:2.5:9 ratio.|[0031] The dry material and biochar were mixed in a stirrer at low speed 140 rpm for 3 min followed by high speed mixing at 280rpm for 1min, then mixing water was added, then mixed at low speed 3 min, and mixed at high speed at 280rpm for 3 min. After the mixing is completed, pouring the fresh mixture into a mould with the size of 40mm multiplied by 40mm multiplied by 40mm, vibrating the mould on a vibrating table for 10 times to avoid the biochar floating on the upper layer of the test block, and fully stirring the slurry by using a stirring rod to release bubbles from the slurry so as to ensure the stability of the test of the sample.|[0032] These samples were subjected to in-mold pretreatment for 24 hours and then to a release treatment. The temperature and Relative Humidity (RH) of the pretreatment were 20℃and 95%, respectively. The purpose of the pretreatment is to remove excess free water from the sample. The free moisture prevents the diffusion of gaseous CO2 in the cement matrix, but may also provide the necessary water reaction conditions for the relevant reactions. The demolded sample is placed in an oxidation chamber and cured to a selected test time. The compressive strength of the cement mortar is measured by adopting a STYE-300C compressive strength tester, and the loading rate is 1.4 kN/s. Each set of experiments was run three times and the average was determined as the final result. After curing for 7 days and 28 days, the compressive properties of the corresponding cement test blocks were tested.|[0033] As shown in the results of FIG. 1, the mechanical properties of the moso bamboo added with no additive are improved to a certain extent, the mechanical properties are obviously improved after the iron oxide or the biochar prepared by the co-pyrolysis of the phosphoric acid and the moso bamboo is added, the mechanical properties are highest after the biochar prepared by the co-pyrolysis of the phosphoric acid and the iron oxide and the moso bamboo is added, and the mechanical properties reach 40.8KN in 7 days and 55.8KN in 28 days.|[0034] The added phosphoric acid and ferric oxide act together to stimulate hydration reaction in the cement slurry, and the excellent pore structure in the prepared biochar is added, so that the mechanical property of cement is greatly improved.|[0035] Furthermore, as can be seen from the X-ray diffraction pattern of the co-pyrolysis product of fig. 2, since the carbon material under the pyrolysis is of an amorphous structure, all diffraction peaks can be attributed to the decomposition products of Fe and P. In the biochar added with Fe2O3, the diffraction peak is consistent with the standard card of Fe3O4, which is consistent with the product distribution and pyrolysis behavior of the pyrolysis process, and further indicates that Fe2O3 has little influence on the carbon retention rate under the pyrolysis of low temperature.|[0036] While a diffraction peak of the biochar prepared by adding phosphoric acid is observed at a position of 21 degrees 2 theta, a large broad peak is corresponding to 002 strips of a graphite structure, and the result of the broad peak shows that the biochar prepared by phosphoric acid is of an amorphous structure.|[0037] The diffraction peak intensity of the biochar prepared under the synergistic effect is obviously reduced, compared with the biochar prepared by adding ferric oxide, the peak intensity reduction and the disappearance of one diffraction peak are observed at the position of 36 degrees of 2 theta, which indicates that the oxidation-reduction reaction of iron and coke is slowed down in the pyrolysis process, and further proves that the synergistic effect of phosphoric acid and ferric oxide can reduce the carbon loss in the pyrolysis process.|[0038] The diffraction peaks of the biochar prepared by co-pyrolysis of the ferric phosphate and the moso bamboo are completely different, and further prove that the ferric phosphate and the ferric oxide do not generate double decomposition reaction to generate the ferric phosphate.|[0039] As can be seen from the Fourier infrared spectra of the different biochars shown in FIG. 3, the broad peaks observed at (3200-3700 cm-1) of the prepared biochars are characteristic of stretching vibration of hydroxyl (-OH) groups in hydrogen bonds from carboxyl groups, phenol or alcohol and water. In some cases it may also correspond to N-H stretching vibrations in the amino compound. The peaks observed at (2800-3000 cm-1) may indicate the presence of saturated symmetrical and asymmetrical aliphatic C-H stretching vibrations. The two peaks at 1594 and 1624 can be attributed to the stretching vibration of c=c, c=o in ketones, quinones, aldehydes, lactones and ketones. The peak in the spectral region between 1150cm-1 and 950cm-1 is attributed to the functional group formed by phosphate and biochar. Biochar prepared using phosphoric acid and ferric phosphate is attributable to symmetrical phosphate (PO 2-) stretching at 1089cm-1, i.e., stretching vibration of the phosphate groups. Since the spectral peak wavelength of P-O-C is shorter than that of the symmetrical phosphate (PO 2-) and is attributable to P-O-C at 1025cm-1 and 943cm-1, a distinct band was observed for biochar prepared by treatment with phosphoric acid and synergy.|[0040] The crosslinking reaction is the primary mechanism to retain C in the solid phase, and this result suggests that the reaction of biomass with H3PO4 may lead to the formation of cellulose phosphate, and the possible presence of C-O-PO3 type groups (i.e., (CO) 3PO, (CO) 2 PO2 and (CO) PO 3) may physically protect the C structure, thereby reducing C losses that do not occur with biochar produced from ferric phosphate.|[0041] At 560cm-1, which is attributable to Fe-O-C, this crosslinking reaction is effective in retaining C in the char. Meanwhile, the previous research results show that Fe ions can interact with oxygen-containing groups in the organic framework and then be converted into inorganic oxides.|[0042] This result indicates that fe—o complexes or iron oxides may be present on the surface. The peak intensity of the biochar prepared under the synergistic effect of 1025cm < -1 > and 943cm < -1 > is higher, namely the content of P-O-C is increased, and the added Fe possibly catalyzes the reaction of P, so that more P-O-C is obtained in the biochar to wrap more C, and more carbon is sealed in the biochar.|[0043] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.|[0044] In the description of the present specification, reference to the terms "one embodiment," "some embodiments," "illustrative embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples.|[0045] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the spirit and scope of the invention as defined by the appended claims and their equivalents. Family Number|(117027433)|117027433|Abstract|(CN121107390 A)|The present invention discloses a carbon sequestration biochar and a preparation method thereof , the preparation method comprises : adding crushed biomass into a carbon sequestration agent solution to obtain a first mixture , the carbon sequestration agent comprising phosphoric acid and / or iron oxide ; drying the first mixture , and grinding to obtain a powdery second mixture ; and pyrolyzing the second mixture in an inert gas atmosphere to obtain the carbon -sequestered biochar . Therefore , the high - yield and high - carbon - content biochar is prepared through co - pyrolysis of phosphoric acid , ferric oxide and biomass , the carbon sequestration rate of the biochar is increased through the synergistic effect of phosphoric acid and ferric oxide , a physical barrier is formed on the surface of the biochar , the oxidation resistance and biomineralization resistance of the biochar are enhanced , and escape of a biomass pyrolysis primary product is limited ; it is thus retained in the carbon matrix , resulting in more carbon retention and high yields . The biochar is applied to cement slurry , and all phosphorus and iron elements contained in the biochar are utilized to stimulate the hydration reaction of cement to improve the mechanical property . |CPC codes|(CN121107390 A)|B01D - 053/02 |B01D - 2253/102 |B01D - 2257/304 |B01D - 2257/7025 |B01D - 2257/708 |B01J - 020/02/77 |B01J - 020/04/3 |B01J - 020/06 |B01J - 020/10/3 |B01J - 020/10 |B01J - 020/12 |B01J - 020/14 |B01J - 020/20 |B01J - 020/22 |B01J - 020/28/023 |B01J - 020/28/042 |B01J - 020/28/057 |B01J - 020/28/059 |B01J - 020/28 |B01J - 020/30/85 |B01J - 2220/42 |B01J - 2220/4825 |C01B - 032/05 |C01B - 032/318 |C01B - 032/336 |C01P - 2006/12 |C01P - 2006/17 |IPC codes|(CN121107390 A)|B01D - 053/02 |B01J - 020/20 |B01J - 020/30 |C01B - 032/05 |Title|(CN121107390 A)|Carbon sequestration biochar and preparation method thereof | Chemical engineering|Environmental technology|Materials, metallurgy B01D-053/02|B01D-2253/102|B01D-2257/304|B01D-2257/7025|B01D-2257/708|B01J-020/02/77|B01J-020/04/3|B01J-020/06|B01J-020/10|B01J-020/10/3|B01J-020/12|B01J-020/14|B01J-020/20|B01J-020/22|B01J-020/28|B01J-020/28/023|B01J-020/28/042|B01J-020/28/057|B01J-020/28/059|B01J-020/30/85|B01J-2220/42|B01J-2220/4825|B09B-001/00/4|C01B-032/05|C01B-032/318|C01B-032/336|C01P-2006/12|C01P-2006/17|C04B-014/06|Y02C-010/08|Y02P-070/34 B01D-053/02|B01D-2253/102|B01D-2257/304|B01D-2257/7025|B01D-2257/708|B01J-020/02/77|B01J-020/04/3|B01J-020/06|B01J-020/10|B01J-020/10/3|B01J-020/12|B01J-020/14|B01J-020/20|B01J-020/22|B01J-020/28|B01J-020/28/023|B01J-020/28/042|B01J-020/28/057|B01J-020/28/059|B01J-020/30/85|B01J-2220/42|B01J-2220/4825|B09B-001/00/4|C01B-032/05|C01B-032/318|C01B-032/336|C01P-2006/12|C01P-2006/17|C04B-014/06|Y02C-010/08|Y02P-070/34 B01D-053/02|B01J-020/20|B01J-020/30|C01B-032/05|C04B-014/36 B01D-053/02|B01J-020/20|B01J-020/30|C01B-032/05|C04B-014/36 PENDING (CN121107390)|PENDING ALIVE (CN121107390)|ALIVE (CN121107390)|LEGAL DETAILS FOR CN121107390|Actual or expected expiration date=2045-08-22|Legal state=ALIVE|Status=PENDING|Event publication date=2025-08-22|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511179914|Application date=2025-08-22|Standardized application number=2025CN-1179914|Event publication date=2025-12-12|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121107390|Publication stage code=A|Publication date=2025-12-12|Standardized publication number=CN121107390|Event publication date=2025-12-12|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-12-30|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121107390)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfSbSu4PrST6Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080085074&ekey=2024&xpn=CN121107390&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=k1AfZx9IB80IEBZkvz7aoJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121107390)|CN (CN121107390)|NAME=HEFEI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN121107390)|NAME=WANG ZHOUXIN;Hefei Hongshanxin Intellectual Property Agency (General Partnership) , REG=00435 (CN121107390)|CN (CN121107390)|NAME=DIAO RUI, COUNTRY=CN |NAME=HU XU|NAME=LI BOWEN|NAME=YANG CUNZHANG|NAME=QI FENGLEI|NAME=LIU XIAOHAO|NAME=CHA ZHENTING|NAME=ZHANG ZHITAO|NAME=ZHANG SHUANGLIN|NAME=YANG SHUQUAN|NAME=MA PEIYONG 0 1 Titre: (CN121107390)|Carbon sequestration biochar and preparation method thereof Résumé: (CN121107390)|The present invention discloses a carbon sequestration biochar and a preparation method thereof, the preparation method comprises: adding crushed biomass into a carbon sequestration agent solution to obtain a first mixture, the carbon sequestration agent comprising phosphoric acid and/or iron oxide; drying the first mixture, and grinding to obtain a powdery second mixture; and pyrolyzing the second mixture in an inert gas atmosphere to obtain the carbon-sequestered biochar. Therefore, the high-yield and high-carbon-content biochar is prepared through co-pyrolysis of phosphoric acid, ferric oxide and biomass, the carbon sequestration rate of the biochar is increased through the synergistic effect of phosphoric acid and ferric oxide, a physical barrier is formed on the surface of the biochar, the oxidation resistance and biomineralization resistance of the biochar are enhanced, and escape of a biomass pyrolysis primary product is limited; it is thus retained in the carbon matrix, resulting in more carbon retention and high yields. The biochar is applied to cement slurry, and all phosphorus and iron elements contained in the biochar are utilized to stimulate the hydration reaction of cement to improve the mechanical property. 23 Abstract gpt-4o-mini no The article focuses on biochar production and its application in cement, without addressing mineral weathering or CO₂ capture through enhanced weathering processes.
25 CN202423053576U CN202423053576U CN223584808 116779650 CN223584808 U 2025-11-25 [CN223584808U] 2024-12-10 2024-12-10 2025-11-25 (CN223584808U)|2025-11-25 (CN223584808)|2034-12-10 (CN223584808)|Straw smashing and scattering device for crop straw returning and carbon sequestration (CN223584808)|The utility model relates to the technical field of crop straw returning and carbon sequestration, and discloses a straw smashing and scattering device for crop straw returning and carbon sequestration, which comprises a device shell and a feed port, a first driving motor is arranged at the top of the device shell, a first rotating shaft is additionally arranged at the upper part of an inner cavity of the device shell, and a second driving motor is arranged at the lower part of the inner cavity of the device shell. The first rotating shaft is connected with the first driving motor, and crushing blades are additionally arranged on the surface; and crushing rollers are additionally arranged on the two sides of the top of the screening plate, limiting side plates are connected to the two ends of the screening plate, and third driving motors are installed on the outer sides of the limiting side plates. According to the straw smashing and scattering device for crop straw returning to the field and carbon sequestration, straw is guided into the device shell through a feeding port, a first driving motor drives a first rotating shaft and smashing blades to preliminarily smash the passing straw, the straw falls to the top of a screening plate, and the straw with the qualified size falls through the screening plate; and the third driving motor drives the crushing roller to rotate so as to further crush the straws. JIANGSU YANCHENG ENVIRONMENTAL PROTECTION SCIENCE & TECHNOLOGY CITY SOIL ECOLOGY INSTITUTE (CN223584808)|JIANGSU YANCHENG ENVIRONMENTAL PROTECTION SCIENCE AND TECHNOLOGY CITY SOIL ECOLOGY INSTITUTE ZHAO HENGFENG|WANG LIKUN|ZHANG LI (CN223584808)|ZHAO HENGFENG|WANG LIKUN|ZHANG LI (CN223584808)|CUI XUSHEN;Hefei Zuoxin Patent Agency (General Partnership)|Reg. Nb: 34152 (CN223584808)|1. Crop straw returns field and solid carbon with straw crushing throwing device, its characterized in that includes: the device comprises a device shell (1) and feed inlets (2) arranged on two sides of the top of the device shell (1), wherein a first driving motor (5) is arranged in the center of the top of the device shell (1), a first rotating shaft (6) is additionally arranged in the center of the upper part of an inner cavity of the device shell (1) and is coaxially connected with the first driving motor (5), and crushing blades (7) are uniformly arranged on the surface of the first rotating shaft (6); The screening plate (8) is arranged at the center of an inner cavity of the device shell (1), crushing rollers (13) are additionally arranged at two sides of the center of the top of the screening plate (8), two ends of each crushing roller (13) are rotatably connected with limiting side plates (14), and a third driving motor (16) is arranged at the outer side of each limiting side plate (14) and is coaxially connected with each crushing roller (13); The bidirectional screw rod (9) is arranged at the lower part of the center of the front side and the back side of the device shell (1), the end part of the bidirectional screw rod (9) is coaxially connected with a second driving motor (10), sliding blocks (11) are sleeved on two sides of the center of the bidirectional screw rod (9), connecting plates (12) are arranged at the tops of the sliding blocks (11), and the connecting plates (12) are connected with the bottoms of limiting side plates (14). | (CN223584808)|The utility model relates to the technical field of crop straw returning and carbon fixation, and discloses a straw crushing and throwing device for crop straw returning and carbon fixation, which comprises a device shell and a feeding hole, wherein a first driving motor is arranged at the top of the device shell, a first rotating shaft is additionally arranged at the upper part of an inner cavity of the device shell and is connected with the first driving motor, and a crushing blade is additionally arranged on the surface of the first rotating shaft; screening board, and top both sides add and are equipped with crushing roller to be connected with spacing curb plate in both ends, and the third driving motor is installed in the outside of spacing curb plate. This crop straw is straw crushing throwing device for still field solid carbon, inside with straw introduction device casing through the feed inlet, first driving motor drives first pivot and smashes the blade and preliminary smash the straw that passes through, and the straw whereabouts is to the top of screening board, and the size is qualified straw passes through screening board decline, and third driving motor drives crushing roller rotation, further smashes the straw.| (CN223584808)|STRAW(100,51)|STRAW CRUSHING(100,19)|CARBON FIXING STRAW CRUSHING(100,1)|CROP STRAW RETURNING(81,4)|BIDIRECTIONAL SCREW ROD(76,4)|STRAW WHEREABOUTS(75,1)|SCREENING BOARD DECLINE(65,1)|PRELIMINARY SMASH(62,1)|CROP STRAW(60,8)|CRUSHING ROLLER(51,19)|DRIVING MOTOR(50,32)|SCREENING BOARD(46,4)|STRAW INTRODUCTION(44,2)|DEVICE SHELL(39,29)|STRAW RETURN(39,1)|BIDIRECTIONAL SCREW ROD CENTER(35,1)|INNER CAVITY(33,11)|CRUSHING BLADE(30,7)|CARBON FIXATION(27,13)|SMASH(27,2)|ROLLER ROTATION(27,1)|SCREEN PLATE(25,18)|FEED INLET(24,10)|SOLID CARBON(23,3)|FEED HOLE(23,2)|ROTATING SHAFT(20,32)|DISCHARGE HOLE(18,6)|RETURNING CROP STRAW(17,5)|CURB PLATE(17,3)|SCREENING BOARD TOP(16,3)|STRAW QUALIFICATION(15,5)|DISCHARGE PORT(14,3)|STRAW RETURN FIELD(14,1)|FEEDING HOPPER(13,7)|DRIVING MOTOR DRIVE(12,9)|SLIDING BLOCK(9,10)|EXTENSION PLATE(9,3)|CRUSHED STRAW THROWING DISTANCE(9,2)|SLIDABLE CONNECTION(9,2)|MOTOR DRIVE(8,9)|PARTLY UNQUALIFIED STRAW(8,1)|GUIDE PLATE(7,13)|FIXING CARBON(6,5)|BI DIRECTIONAL SCREW ROD(6,3)|PASSED STRAW(6,3)|ABUNDANT RESOURCE(6,1)|COMPREHENSIVE CRUSHING TREATMENT(6,1)|DECLINE QUALIFICATION(6,1)|NONEXCLUSIVE INCLUSION(6,1)|INCLINED PLANE(5,5)|BLOCKAGE(5,3)|EPITAXIAL PLATE(5,3)|FEED HOPPER(5,2)|SIZE QUALIFIED STRAW(5,2)|STRAW REMAINS(5,2)|CROP MATURING(5,1)|PRELIMINARY CRUSHING(5,1)|OUTER SIDE(4,9)|DECOMPOSITION(4,2)|SCATTERING(4,2)|ACCESSIBLE SCREENING(4,1)|LIMITING SIDE PLATE(3,24)|SCREENING PLATE TOP(3,5)|GROUND(3,4)|BIDIRECTIONAL SCREW CENTER(3,1)|DISCHARGING HOLE(3,1)|KEY LINK(3,1)|LINKING BOARD(3,1)|RELATIONAL TERM(3,1)|STEM TERM(3,1)|AUXILIARY COMPONENT(2,1)|BAFFLE(2,1)| (CN223584808)|1. Crop straw returns field and solid carbon with straw crushing throwing device, its characterized in that includes:| the device comprises a device shell (1) and feed inlets (2) arranged on two sides of the top of the device shell (1), wherein a first driving motor (5) is arranged in the center of the top of the device shell (1), a first rotating shaft (6) is additionally arranged in the center of the upper part of an inner cavity of the device shell (1) and is coaxially connected with the first driving motor (5), and crushing blades (7) are uniformly arranged on the surface of the first rotating shaft (6); | The screening plate (8) is arranged at the center of an inner cavity of the device shell (1), crushing rollers (13) are additionally arranged at two sides of the center of the top of the screening plate (8), two ends of each crushing roller (13) are rotatably connected with limiting side plates (14), and a third driving motor (16) is arranged at the outer side of each limiting side plate (14) and is coaxially connected with each crushing roller (13); | The bidirectional screw rod (9) is arranged at the lower part of the center of the front side and the back side of the device shell (1), the end part of the bidirectional screw rod (9) is coaxially connected with a second driving motor (10), sliding blocks (11) are sleeved on two sides of the center of the bidirectional screw rod (9), connecting plates (12) are arranged at the tops of the sliding blocks (11), and the connecting plates (12) are connected with the bottoms of limiting side plates (14). |2. The straw crushing and throwing device for crop straw returning to the field and carbon fixation according to claim 1 is characterized in that feeding hoppers (3) are arranged on two sides of the top of the device shell (1), and the feeding hoppers (3) are communicated with the feeding inlet (2).|3. The straw crushing and throwing device for crop straw returning to field and carbon fixation according to claim 1, wherein a discharge hole (4) is additionally arranged at the lower part of the outer side of the device shell (1), a second rotating shaft (17) is additionally arranged at the outer end of the discharge hole (4), and the second rotating shaft (17) is rotationally connected with the device shell (1).|4. The straw crushing and throwing device for crop straw returning and carbon fixation according to claim 3, wherein the periphery of the outer surface of the second rotating shaft (17) is provided with a throwing side plate (18), and the back surface of the second rotating shaft (17) is coaxially connected with a fourth driving motor (19).|5. The straw crushing and throwing device for crop straw returning to field and carbon fixation according to claim 1, wherein the limiting side plate (14) is in sliding connection with the device shell (1), and an extension plate (15) is transversely arranged on the outer side of the limiting side plate (14).|6. The straw crushing and throwing device for crop straw returning to field and carbon fixation according to claim 3 is characterized in that a guide plate (20) is arranged at the lower part of an inner cavity of the device shell (1), the top of the guide plate (20) is designed as an inclined plane, and the bottom end of the inclined plane at the top of the guide plate (20) corresponds to the discharge port (4). (CN223584808)|TECHNICAL FIELD|Technical Field|[0001] The utility model relates to the technical field of crop straw returning and carbon fixation, in particular to a straw crushing and throwing device for crop straw returning and carbon fixation.|BACKGROUND ART|[0002] Crop straw refers to the general term of the stem and leaf part remained after crop maturing and threshing in the agricultural production process. It is a by-product in agricultural production, and has abundant resource quantity and wide application. Crop straw returning and carbon fixation are important agricultural environmental protection measures, and aim to increase the organic matter content of soil, improve the soil fertility and simultaneously realize carbon fixation and emission reduction by returning the straw to the soil. Crop straw returning to the field and carbon fixation are needed to be crushed and thrown. This step is one of the key links in the straw returning and carbon fixing technology, and aims to improve the decomposition efficiency and carbon fixing effect of the straw in the soil.|[0003] The common straw crushing and throwing device for returning crop straws to fields and fixing carbon is generally composed of a shell, a crushing device, a throwing device, a transmission device, other auxiliary components and the like. Firstly, straw is led into a shell, the straw is crushed by a crushing device, the crushed straw is uniformly scattered on the surface of a farmland by a scattering device and covered on soil, and a transmission device is responsible for transmitting external power to the crushing device and the scattering device.|[0004] Traditional crop straw is straw crushing and throwing device for still field solid carbon, the reducing mechanism who uses is crushing blade usually, and crushing blade installs in the pivot, and the pivot is driven by the motor for crushing blade smashes the straw that passes through, only through crushing blade to straw smash thoroughly inadequately, the straw piece of exhaust hardly enters into in the soil, makes the decomposition rate of straw piece slow down. In order to solve the problems, part of crop straws are returned to the field and carbon is crushed and thrown by the straw crushing and throwing device, two groups of crushing structures are additionally arranged in the device, and after the straws are primarily crushed, the straws are further crushed. However, in the mode, though the crushing effect on the straw can be improved through the two groups of crushing devices, the phenomenon that part of straw is not crushed thoroughly still occurs in the crushing process. Therefore, the straw crushing and throwing device for returning crop straws to fields and fixing carbon is provided.|DISCLOSURE|Disclosure of utility model|[0005] (One) solving the technical problems|[0006] Aiming at the defects of the prior art, the utility model provides a straw crushing and scattering device for returning crop straws to fields and fixing carbon, which aims to solve the technical problem that partial straw crushing is not thorough.|[0007] (II) technical scheme|[0008] In order to achieve the purpose, the utility model provides the following technical scheme that the straw crushing and throwing device for crop straw returning and carbon fixation comprises the following components:|[0009] The device comprises a device shell and feed inlets arranged on two sides of the top of the device shell, wherein a first driving motor is arranged in the center of the top of the device shell, a first rotating shaft is additionally arranged in the center of the upper part of an inner cavity of the device shell and is coaxially connected with the first driving motor, and crushing blades are uniformly arranged on the surface of the first rotating shaft; |[0010] The screening plate is arranged at the center of an inner cavity of the device shell, crushing rollers are additionally arranged on two sides of the center of the top of the screening plate, two ends of each crushing roller are rotatably connected with limiting side plates, and the outer sides of the limiting side plates are provided with third driving motors and are coaxially connected with the crushing rollers; |[0011] The bidirectional screw is arranged at the lower part of the center of the front side and the back side of the device shell, the end part of the bidirectional screw is coaxially connected with a second driving motor, the two sides of the center of the bidirectional screw are sleeved with sliding blocks, the top of each sliding block is provided with a connecting plate, and the connecting plates are connected with the bottoms of the limiting side plates. The straw is guided into the inside of the device shell through the feed inlet, the first driving motor drives the first rotating shaft and the crushing blade to primarily crush the passed straw, the straw falls to the top of the screening plate, the qualified straw of the size descends through the screening plate, the third driving motor drives the crushing roller to rotate on the limiting side plate and further crush the straw at the top of the screening plate, the second driving motor drives the bidirectional screw to rotate, and the sliding block drives the crushing roller to move in opposite directions through the connecting plate and the limiting side plate and adjusts the interval between the two groups of crushing rollers. On one hand, the screening plate can intercept part of unqualified straws and crush the straws, so that the straws are crushed and qualified to decline, the phenomenon that part of straws are not crushed thoroughly and decline along with qualified straws is avoided, and on the other hand, compared with a traditional fixed crushing structure, the crushing roller with the structure can perform position adjustment, so that the straws at the top of the screening plate can be subjected to comprehensive crushing treatment and collide and move, and the straws are prevented from being accumulated at the top of the screening plate to cause blockage. |[0012] Preferably, the feeding hopper is arranged on two sides of the top of the device shell, and the feeding hopper is communicated with the feeding hole. Straw can be conveyed into the device shell through the feed hopper and the feed inlet.|[0013] Preferably, a discharge hole is additionally arranged at the lower part of the outer side of the device shell, a second rotating shaft is additionally arranged at the outer end of the discharge hole, and the second rotating shaft is rotationally connected with the device shell. The second rotating shaft rotates on the device housing.|[0014] Preferably, a throwing side plate is arranged around the outer surface of the second rotating shaft, and the back surface of the second rotating shaft is coaxially connected with a fourth driving motor. After the crushed straw moves to the throwing side plate, the fourth driving motor drives the throwing side plate to rotate through the second rotating shaft, and the throwing operation is performed on the crushed straw, so that the throwing distance of the crushed straw can be adjusted according to the speed of the fourth driving motor driving the second rotating shaft.|[0015] Preferably, the limiting side plate is in sliding connection with the device shell, and the outer side of the limiting side plate is transversely provided with the extension plate. The limiting side plate can drive the epitaxial plate to translate along the device shell.|[0016] Preferably, a guide plate is installed at the lower part of the inner cavity of the device shell, the top of the guide plate is designed into an inclined plane, and the bottom end of the inclined plane at the top of the guide plate corresponds to the discharge hole. After the crushed straw falls to the top of the guide plate and rolls along the inclined plane of the guide plate, the crushed straw can move outwards through the discharge hole, and the phenomenon that part of straw remains in the inner cavity of the shell of the device is avoided.|[0017] (III) beneficial effects|[0018] Compared with the prior art, the utility model provides the straw crushing and scattering device for returning crop straws to fields and fixing carbon, which has the following beneficial effects:|[0019] This crop straw is straw crushing throwing device for still solid carbon in field, inside with straw introduction device casing through the feed inlet, first driving motor drives first pivot and crushing blade and carries out preliminary crushing to the straw of passing through, the straw then falls to the top of screening board, the size qualified straw passes through screening board and descends, third driving motor drives crushing roller and rotates on spacing curb plate, and further smash the processing to the straw at screening board top, accessible screening board intercepts the partly unqualified straw, and carry out crushing processing, make straw smash qualified decline, avoid appearing partial straw smash incomplete and take place along with the phenomenon that qualified straw descends, the second driving motor drives two-way lead screw rotation, the slider then drives crushing roller through linking board and spacing curb plate and moves in opposite directions, and adjust the interval between the two sets of crushing rollers. Compared with the traditional fixed crushing structure, the crushing roller of the structure can carry out position adjustment, so that the straws at the top of the screening plate can be comprehensively crushed, and the straws are collided and moved, so that the straws are prevented from being accumulated at the top of the screening plate to cause blockage. |DRAWINGS DESCRIPTION|[0020] FIG. 1 is a schematic diagram of the overall structure of the present utility model;|[0021] FIG. 2 is a schematic cross-sectional view of a housing of the device of the present utility model; |[0022] FIG. 3 is a schematic view of a bi-directional screw and its connection structure according to the present utility model; |[0023] Fig. 4 is a schematic diagram of a second shaft and a connection structure thereof according to the present utility model. |[0024] The device comprises a device shell, a feeding hole, a feeding hopper, a discharging hole, a first driving motor, a first rotating shaft, a crushing blade, a screening plate, a 9, a bidirectional screw rod, a 10, a second driving motor, a 11, a sliding block, a 12, a connecting plate, a 13, a crushing roller, a 14, a limiting side plate, a 15, an epitaxial plate, a 16, a third driving motor, a 17, a second rotating shaft, a 18, a throwing side plate, a 19, a fourth driving motor, a 20 and a guide plate.|INVENTION MODE|Detailed Description|[0025] The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.|[0026] The utility model provides a technical scheme, which relates to a straw crushing and throwing device for returning crop straws to fields and fixing carbon, comprising a device shell 1 and feed inlets 2 arranged on two sides of the top of the device shell 1, wherein a first driving motor 5 is arranged in the center of the top of the device shell 1, a first rotating shaft 6 is additionally arranged in the center of the upper part of an inner cavity of the device shell 1 and is coaxially connected with the first driving motor 5, and crushing blades 7 are uniformly arranged on the surface of the first rotating shaft 6;|[0027] Referring to fig. 2, a screening plate 8 is disposed at the center of an inner cavity of a device housing 1, two sides of the center of the top of the screening plate 8 are additionally provided with crushing rollers 13, two ends of each crushing roller 13 are rotatably connected with a limiting side plate 14, and the outer side of each limiting side plate 14 is provided with a third driving motor 16 and is coaxially connected with each crushing roller 13; |[0028] Referring to fig. 3, a bi-directional screw rod 9 is disposed at the lower part of the center of the front and back surfaces of the device housing 1, and the end of the bi-directional screw rod 9 is coaxially connected with a second driving motor 10, two sides of the center of the bi-directional screw rod 9 are sleeved with sliding blocks 11, the top of the sliding blocks 11 is provided with a connecting plate 12, and the connecting plate 12 is connected with the bottom of a limiting side plate 14. Straw is guided into the inside of the device shell 1 through the feed inlet 2, the first driving motor 5 drives the first rotating shaft 6 and the crushing blade 7 to primarily crush the passed straw, the straw falls to the top of the screening plate 8, the qualified straw descends through the screening plate 8, the third driving motor 16 drives the crushing roller 13 to rotate on the limiting side plate 14, the straw at the top of the screening plate 8 is further crushed, the second driving motor 10 drives the bidirectional screw 9 to rotate, the sliding block 11 drives the crushing roller 13 to move in opposite directions through the connecting plate 12 and the limiting side plate 14, and the interval between the two groups of crushing rollers 13 is adjusted. On one hand, partial unqualified straws can be intercepted through the screening plate 8 and crushed, so that the straws are crushed and qualified to decline, the phenomenon that partial straws are not crushed thoroughly and decline along with qualified straws is avoided, and on the other hand, compared with a traditional fixed crushing structure, the position of the crushing roller 13 of the structure can be adjusted, so that the straws at the top of the screening plate 8 can be comprehensively crushed and collided and moved, and the straws are prevented from being accumulated at the top of the screening plate 8 to cause blockage. |[0029] Referring to fig. 1, feeding hoppers 3 are mounted on two sides of the top of a device housing 1, and the feeding hoppers 3 are connected with a feeding inlet 2 in a communicating manner. Straw can be conveyed into the device shell 1 through the feed hopper 3 and the feed inlet 2.|[0030] Referring to fig. 2, a discharge port 4 is additionally arranged at the lower part of the outer side of the device housing 1, and a second rotating shaft 17 is additionally arranged at the outer end of the discharge port 4, and the second rotating shaft 17 is rotatably connected with the device housing 1. The second rotating shaft 17 rotates on the apparatus housing 1.|[0031] Referring to fig. 4, a spreading side plate 18 is installed around the outer surface of the second rotating shaft 17, and a fourth driving motor 19 is coaxially connected to the back surface of the second rotating shaft 17. After the crushed straw moves to the throwing side plate 18, the fourth driving motor 19 drives the throwing side plate 18 to rotate through the second rotating shaft 17, and the throwing operation is performed on the crushed straw, so that the throwing distance of the crushed straw can be adjusted according to the speed of the fourth driving motor 19 driving the second rotating shaft 17.|[0032] Referring to fig. 2, the limiting side plate 14 is slidably connected to the device housing 1, and an extension plate 15 is transversely mounted on the outer side of the limiting side plate 14. The limiting side plate 14 can drive the epitaxial plate 15 to translate along the device housing 1. The baffle 20 is installed to the inner chamber lower part of device casing 1, and the top of baffle 20 is the inclined plane design, and the bottom of baffle 20 top inclined plane corresponds with discharge gate 4. After the crushed straw falls to the top of the guide plate 20 and rolls along the inclined plane of the guide plate 20, the crushed straw moves outwards through the discharge hole 4, and the phenomenon that part of straw remains in the inner cavity of the device shell 1 is avoided.|[0033] The technical scheme is that straws are guided into a device shell 1 through a feed inlet 2, a first driving motor 5 drives a first rotating shaft 6 and a crushing blade 7 to primarily crush the passed straws, the straws fall to the top of a screening plate 8, the qualified straws descend through the screening plate 8, a third driving motor 16 drives a crushing roller 13 to rotate on a limiting side plate 14 and further crush the straws on the top of the screening plate 8, a second driving motor 10 drives a bidirectional screw 9 to rotate, a sliding block 11 drives the crushing roller 13 to move oppositely through a connecting plate 12 and the limiting side plate 14, and the interval between two groups of crushing rollers 13 is adjusted. After the crushed straw falls to the top of the guide plate 20 and rolls along the inclined plane of the guide plate 20, the crushed straw outwards moves through the discharge hole 4, and after the crushed straw moves to the throwing side plate 18, the fourth driving motor 19 drives the throwing side plate 18 to rotate through the second rotating shaft 17, and the throwing operation is performed on the crushed straw.|[0034] It is noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.|[0035] Although embodiments of the present utility model have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents. (CN223584808)|TECHNICAL FIELD|Technical Field|[0001] The utility model relates to the technical field of crop straw returning and carbon fixation, in particular to a straw crushing and throwing device for crop straw returning and carbon fixation.|BACKGROUND ART|[0002] Crop straw refers to the general term of the stem and leaf part remained after crop maturing and threshing in the agricultural production process. It is a by-product in agricultural production, and has abundant resource quantity and wide application. Crop straw returning and carbon fixation are important agricultural environmental protection measures, and aim to increase the organic matter content of soil, improve the soil fertility and simultaneously realize carbon fixation and emission reduction by returning the straw to the soil. Crop straw returning to the field and carbon fixation are needed to be crushed and thrown. This step is one of the key links in the straw returning and carbon fixing technology, and aims to improve the decomposition efficiency and carbon fixing effect of the straw in the soil.|[0003] The common straw crushing and throwing device for returning crop straws to fields and fixing carbon is generally composed of a shell, a crushing device, a throwing device, a transmission device, other auxiliary components and the like. Firstly, straw is led into a shell, the straw is crushed by a crushing device, the crushed straw is uniformly scattered on the surface of a farmland by a scattering device and covered on soil, and a transmission device is responsible for transmitting external power to the crushing device and the scattering device.|[0004] Traditional crop straw is straw crushing and throwing device for still field solid carbon, the reducing mechanism who uses is crushing blade usually, and crushing blade installs in the pivot, and the pivot is driven by the motor for crushing blade smashes the straw that passes through, only through crushing blade to straw smash thoroughly inadequately, the straw piece of exhaust hardly enters into in the soil, makes the decomposition rate of straw piece slow down. In order to solve the problems, part of crop straws are returned to the field and carbon is crushed and thrown by the straw crushing and throwing device, two groups of crushing structures are additionally arranged in the device, and after the straws are primarily crushed, the straws are further crushed. However, in the mode, though the crushing effect on the straw can be improved through the two groups of crushing devices, the phenomenon that part of straw is not crushed thoroughly still occurs in the crushing process. Therefore, the straw crushing and throwing device for returning crop straws to fields and fixing carbon is provided.|DISCLOSURE|Disclosure of utility model|[0005] (One) solving the technical problems|[0006] Aiming at the defects of the prior art, the utility model provides a straw crushing and scattering device for returning crop straws to fields and fixing carbon, which aims to solve the technical problem that partial straw crushing is not thorough.|[0007] (II) technical scheme|[0008] In order to achieve the purpose, the utility model provides the following technical scheme that the straw crushing and throwing device for crop straw returning and carbon fixation comprises the following components:|[0009] The device comprises a device shell and feed inlets arranged on two sides of the top of the device shell, wherein a first driving motor is arranged in the center of the top of the device shell, a first rotating shaft is additionally arranged in the center of the upper part of an inner cavity of the device shell and is coaxially connected with the first driving motor, and crushing blades are uniformly arranged on the surface of the first rotating shaft; |[0010] The screening plate is arranged at the center of an inner cavity of the device shell, crushing rollers are additionally arranged on two sides of the center of the top of the screening plate, two ends of each crushing roller are rotatably connected with limiting side plates, and the outer sides of the limiting side plates are provided with third driving motors and are coaxially connected with the crushing rollers; |[0011] The bidirectional screw is arranged at the lower part of the center of the front side and the back side of the device shell, the end part of the bidirectional screw is coaxially connected with a second driving motor, the two sides of the center of the bidirectional screw are sleeved with sliding blocks, the top of each sliding block is provided with a connecting plate, and the connecting plates are connected with the bottoms of the limiting side plates. The straw is guided into the inside of the device shell through the feed inlet, the first driving motor drives the first rotating shaft and the crushing blade to primarily crush the passed straw, the straw falls to the top of the screening plate, the qualified straw of the size descends through the screening plate, the third driving motor drives the crushing roller to rotate on the limiting side plate and further crush the straw at the top of the screening plate, the second driving motor drives the bidirectional screw to rotate, and the sliding block drives the crushing roller to move in opposite directions through the connecting plate and the limiting side plate and adjusts the interval between the two groups of crushing rollers. On one hand, the screening plate can intercept part of unqualified straws and crush the straws, so that the straws are crushed and qualified to decline, the phenomenon that part of straws are not crushed thoroughly and decline along with qualified straws is avoided, and on the other hand, compared with a traditional fixed crushing structure, the crushing roller with the structure can perform position adjustment, so that the straws at the top of the screening plate can be subjected to comprehensive crushing treatment and collide and move, and the straws are prevented from being accumulated at the top of the screening plate to cause blockage. |[0012] Preferably, the feeding hopper is arranged on two sides of the top of the device shell, and the feeding hopper is communicated with the feeding hole. Straw can be conveyed into the device shell through the feed hopper and the feed inlet.|[0013] Preferably, a discharge hole is additionally arranged at the lower part of the outer side of the device shell, a second rotating shaft is additionally arranged at the outer end of the discharge hole, and the second rotating shaft is rotationally connected with the device shell. The second rotating shaft rotates on the device housing.|[0014] Preferably, a throwing side plate is arranged around the outer surface of the second rotating shaft, and the back surface of the second rotating shaft is coaxially connected with a fourth driving motor. After the crushed straw moves to the throwing side plate, the fourth driving motor drives the throwing side plate to rotate through the second rotating shaft, and the throwing operation is performed on the crushed straw, so that the throwing distance of the crushed straw can be adjusted according to the speed of the fourth driving motor driving the second rotating shaft.|[0015] Preferably, the limiting side plate is in sliding connection with the device shell, and the outer side of the limiting side plate is transversely provided with the extension plate. The limiting side plate can drive the epitaxial plate to translate along the device shell.|[0016] Preferably, a guide plate is installed at the lower part of the inner cavity of the device shell, the top of the guide plate is designed into an inclined plane, and the bottom end of the inclined plane at the top of the guide plate corresponds to the discharge hole. After the crushed straw falls to the top of the guide plate and rolls along the inclined plane of the guide plate, the crushed straw can move outwards through the discharge hole, and the phenomenon that part of straw remains in the inner cavity of the shell of the device is avoided.|[0017] (III) beneficial effects|[0018] Compared with the prior art, the utility model provides the straw crushing and scattering device for returning crop straws to fields and fixing carbon, which has the following beneficial effects:|[0019] This crop straw is straw crushing throwing device for still solid carbon in field, inside with straw introduction device casing through the feed inlet, first driving motor drives first pivot and crushing blade and carries out preliminary crushing to the straw of passing through, the straw then falls to the top of screening board, the size qualified straw passes through screening board and descends, third driving motor drives crushing roller and rotates on spacing curb plate, and further smash the processing to the straw at screening board top, accessible screening board intercepts the partly unqualified straw, and carry out crushing processing, make straw smash qualified decline, avoid appearing partial straw smash incomplete and take place along with the phenomenon that qualified straw descends, the second driving motor drives two-way lead screw rotation, the slider then drives crushing roller through linking board and spacing curb plate and moves in opposite directions, and adjust the interval between the two sets of crushing rollers. Compared with the traditional fixed crushing structure, the crushing roller of the structure can carry out position adjustment, so that the straws at the top of the screening plate can be comprehensively crushed, and the straws are collided and moved, so that the straws are prevented from being accumulated at the top of the screening plate to cause blockage. |DRAWINGS DESCRIPTION|[0020] FIG. 1 is a schematic diagram of the overall structure of the present utility model;|[0021] FIG. 2 is a schematic cross-sectional view of a housing of the device of the present utility model; |[0022] FIG. 3 is a schematic view of a bi-directional screw and its connection structure according to the present utility model; |[0023] Fig. 4 is a schematic diagram of a second shaft and a connection structure thereof according to the present utility model. |[0024] The device comprises a device shell, a feeding hole, a feeding hopper, a discharging hole, a first driving motor, a first rotating shaft, a crushing blade, a screening plate, a 9, a bidirectional screw rod, a 10, a second driving motor, a 11, a sliding block, a 12, a connecting plate, a 13, a crushing roller, a 14, a limiting side plate, a 15, an epitaxial plate, a 16, a third driving motor, a 17, a second rotating shaft, a 18, a throwing side plate, a 19, a fourth driving motor, a 20 and a guide plate.|INVENTION MODE|Detailed Description|[0025] The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.|[0026] The utility model provides a technical scheme, which relates to a straw crushing and throwing device for returning crop straws to fields and fixing carbon, comprising a device shell 1 and feed inlets 2 arranged on two sides of the top of the device shell 1, wherein a first driving motor 5 is arranged in the center of the top of the device shell 1, a first rotating shaft 6 is additionally arranged in the center of the upper part of an inner cavity of the device shell 1 and is coaxially connected with the first driving motor 5, and crushing blades 7 are uniformly arranged on the surface of the first rotating shaft 6;|[0027] Referring to fig. 2, a screening plate 8 is disposed at the center of an inner cavity of a device housing 1, two sides of the center of the top of the screening plate 8 are additionally provided with crushing rollers 13, two ends of each crushing roller 13 are rotatably connected with a limiting side plate 14, and the outer side of each limiting side plate 14 is provided with a third driving motor 16 and is coaxially connected with each crushing roller 13; |[0028] Referring to fig. 3, a bi-directional screw rod 9 is disposed at the lower part of the center of the front and back surfaces of the device housing 1, and the end of the bi-directional screw rod 9 is coaxially connected with a second driving motor 10, two sides of the center of the bi-directional screw rod 9 are sleeved with sliding blocks 11, the top of the sliding blocks 11 is provided with a connecting plate 12, and the connecting plate 12 is connected with the bottom of a limiting side plate 14. Straw is guided into the inside of the device shell 1 through the feed inlet 2, the first driving motor 5 drives the first rotating shaft 6 and the crushing blade 7 to primarily crush the passed straw, the straw falls to the top of the screening plate 8, the qualified straw descends through the screening plate 8, the third driving motor 16 drives the crushing roller 13 to rotate on the limiting side plate 14, the straw at the top of the screening plate 8 is further crushed, the second driving motor 10 drives the bidirectional screw 9 to rotate, the sliding block 11 drives the crushing roller 13 to move in opposite directions through the connecting plate 12 and the limiting side plate 14, and the interval between the two groups of crushing rollers 13 is adjusted. On one hand, partial unqualified straws can be intercepted through the screening plate 8 and crushed, so that the straws are crushed and qualified to decline, the phenomenon that partial straws are not crushed thoroughly and decline along with qualified straws is avoided, and on the other hand, compared with a traditional fixed crushing structure, the position of the crushing roller 13 of the structure can be adjusted, so that the straws at the top of the screening plate 8 can be comprehensively crushed and collided and moved, and the straws are prevented from being accumulated at the top of the screening plate 8 to cause blockage. |[0029] Referring to fig. 1, feeding hoppers 3 are mounted on two sides of the top of a device housing 1, and the feeding hoppers 3 are connected with a feeding inlet 2 in a communicating manner. Straw can be conveyed into the device shell 1 through the feed hopper 3 and the feed inlet 2.|[0030] Referring to fig. 2, a discharge port 4 is additionally arranged at the lower part of the outer side of the device housing 1, and a second rotating shaft 17 is additionally arranged at the outer end of the discharge port 4, and the second rotating shaft 17 is rotatably connected with the device housing 1. The second rotating shaft 17 rotates on the apparatus housing 1.|[0031] Referring to fig. 4, a spreading side plate 18 is installed around the outer surface of the second rotating shaft 17, and a fourth driving motor 19 is coaxially connected to the back surface of the second rotating shaft 17. After the crushed straw moves to the throwing side plate 18, the fourth driving motor 19 drives the throwing side plate 18 to rotate through the second rotating shaft 17, and the throwing operation is performed on the crushed straw, so that the throwing distance of the crushed straw can be adjusted according to the speed of the fourth driving motor 19 driving the second rotating shaft 17.|[0032] Referring to fig. 2, the limiting side plate 14 is slidably connected to the device housing 1, and an extension plate 15 is transversely mounted on the outer side of the limiting side plate 14. The limiting side plate 14 can drive the epitaxial plate 15 to translate along the device housing 1. The baffle 20 is installed to the inner chamber lower part of device casing 1, and the top of baffle 20 is the inclined plane design, and the bottom of baffle 20 top inclined plane corresponds with discharge gate 4. After the crushed straw falls to the top of the guide plate 20 and rolls along the inclined plane of the guide plate 20, the crushed straw moves outwards through the discharge hole 4, and the phenomenon that part of straw remains in the inner cavity of the device shell 1 is avoided.|[0033] The technical scheme is that straws are guided into a device shell 1 through a feed inlet 2, a first driving motor 5 drives a first rotating shaft 6 and a crushing blade 7 to primarily crush the passed straws, the straws fall to the top of a screening plate 8, the qualified straws descend through the screening plate 8, a third driving motor 16 drives a crushing roller 13 to rotate on a limiting side plate 14 and further crush the straws on the top of the screening plate 8, a second driving motor 10 drives a bidirectional screw 9 to rotate, a sliding block 11 drives the crushing roller 13 to move oppositely through a connecting plate 12 and the limiting side plate 14, and the interval between two groups of crushing rollers 13 is adjusted. After the crushed straw falls to the top of the guide plate 20 and rolls along the inclined plane of the guide plate 20, the crushed straw outwards moves through the discharge hole 4, and after the crushed straw moves to the throwing side plate 18, the fourth driving motor 19 drives the throwing side plate 18 to rotate through the second rotating shaft 17, and the throwing operation is performed on the crushed straw.|[0034] It is noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.|[0035] Although embodiments of the present utility model have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents. Family Number|(116779650)|116779650|Abstract|(CN223584808U U)|The utility model relates to the technical field of crop straw returning and carbon sequestration , and discloses a straw smashing and scattering device for crop straw returning and carbon sequestration , which comprises a device shell and a feed port , a first driving motor is arranged at the top of the device shell , a first rotating shaft is additionally arranged at the upper part of an inner cavity of the device shell , and a second driving motor is arranged at the lower part of the inner cavity of the device shell . The first rotating shaft is connected with the first driving motor , and crushing blades are additionally arranged on the surface ; and crushing rollers are additionally arranged on the two sides of the top of the screening plate , limiting side plates are connected to the two ends of the screening plate , and third driving motors are installed on the outer sides of the limiting side plates . According to the straw smashing and scattering device for crop straw returning to the field and carbon sequestration , straw is guided into the device shell through a feeding port , a first driving motor drives a first rotating shaft and smashing blades to preliminarily smash the passing straw , the straw falls to the top of a screening plate , and the straw with the qualified size falls through the screening plate ; and the third driving motor drives the crushing roller to rotate so as to further crush the straws . |CPC codes|(CN223584808U U)|A01F - 029/00/5 |A01F - 029/04 |A01F - 029/06 |A01F - 029/09 |IPC codes|(CN223584808U U)|A01F - 029/00 |A01F - 029/02 |A01F - 029/09 |Title|(CN223584808U U)|Straw smashing and scattering device for crop straw returning and carbon sequestration | Other special machines A01F-029/00/5|A01F-029/04|A01F-029/06|A01F-029/09 A01F-029/00/5|A01F-029/04|A01F-029/06|A01F-029/09 A01F-029/00|A01F-029/02|A01F-029/09 A01F-029/00|A01F-029/02|A01F-029/09 GRANTED (CN223584808)|GRANTED ALIVE (CN223584808)|ALIVE (CN223584808)|LEGAL DETAILS FOR CN223584808|Actual or expected expiration date=2034-12-10|Legal state=ALIVE|Status=GRANTED|Event publication date=2024-12-10|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202423053576|Application date=2024-12-10|Standardized application number=2024CN-U3053576|Event publication date=2025-11-25|Event code=CN/U|Event indicator=Pos|Event group=Event indicating In Force|Registered Utility Model|Publication country=CN|Publication number=CN223584808|Publication stage code=U|Publication date=2025-11-25|Standardized publication number=CN223584808U|Event publication date=2025-11-25|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN223584808)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=TIBu/CuuJku3fwxfsSlaLqqLeopS8oZMbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000079800035&ekey=2470&xpn=CN223584808U&kind=U https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=q5SNcAmiaYw01YOszpbzg7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN223584808)|NAME=CUI XUSHEN;Hefei Zuoxin Patent Agency (General Partnership) , REG=34152 (CN223584808)|CN (CN223584808)|NAME=ZHAO HENGFENG, COUNTRY=CN |NAME=WANG LIKUN|NAME=ZHANG LI 0 1 Titre: (CN223584808)|Straw smashing and scattering device for crop straw returning and carbon sequestration Résumé: (CN223584808)|The utility model relates to the technical field of crop straw returning and carbon sequestration, and discloses a straw smashing and scattering device for crop straw returning and carbon sequestration, which comprises a device shell and a feed port, a first driving motor is arranged at the top of the device shell, a first rotating shaft is additionally arranged at the upper part of an inner cavity of the device shell, and a second driving motor is arranged at the lower part of the inner cavity of the device shell. The first rotating shaft is connected with the first driving motor, and crushing blades are additionally arranged on the surface; and crushing rollers are additionally arranged on the two sides of the top of the screening plate, limiting side plates are connected to the two ends of the screening plate, and third driving motors are installed on the outer sides of the limiting side plates. According to the straw smashing and scattering device for crop straw returning to the field and carbon sequestration, straw is guided into the device shell through a feeding port, a first driving motor drives a first rotating shaft and smashing blades to preliminarily smash the passing straw, the straw falls to the top of a screening plate, and the straw with the qualified size falls through the screening plate; and the third driving motor drives the crushing roller to rotate so as to further crush the straws. 22 Abstract gpt-4o-mini no The article focuses on a device for processing crop straw for carbon sequestration, but it does not involve the accelerated weathering of minerals or the specific processes related to CO₂ capture and storage as defined.
26 GB202300297|GB2300297|WOGB2024/050026 ARP240100039|WOGB2024/050026|IN202517071665|BR112025014035|JP2025540512|EP24700478|CN202480007137|AU2024206960|CA3279193 BR112025014035|JP2026504057|EP4649146|IN202517071665|CN120548358|BR112025014035|AU2024206960|AR131571|CA3279193|WO2024/149976 110665836 AR131571 A1 2025-04-09 [AR-131571]|WO2024/149976 A1 2024-07-18 [WO2024149976]|IN202517071665 A 2025-10-10 [IN202517071665]|BR112025014035 A2 2026-03-31 [BR112025014035]|BR112025014035 A0 2025-07-22 [BR112025014035]|JP2026504057 A 2026-02-03 [JP2026504057]|EP4649146 A1 2025-11-19 [EP4649146]|CN120548358 A 2025-08-26 [CN120548358]|AU2024206960 A1 2025-07-03 [AU2024206960]|CA3279193 A1 2024-07-18 [CA3279193] 2023-01-09|2024-01-05 2024-01-09|2024-01-05|2025-07-28|2024-01-05|2024-01-05|2024-01-05|2024-01-05|2024-01-05|2024-01-05 2026-03-31|2026-02-03|2025-11-19|2025-10-10|2025-08-26|2025-07-22|2025-07-03|2025-04-09|2024-07-18|2024-07-18 (EP4649146)|2044-01-05|(WO2024/149976)|2026-07-09|(JP2026504057)|2044-01-05|(CN120548358)|2044-01-05|(BR112025014035)|2044-01-05|(IN202517071665)|2044-01-05|(AU2024206960)|2044-01-05|(AR131571)|2044-01-09|(CA3279193)|2044-01-05 (EP4649146)|Carbon sequestration with transgenic plants expressing carbonic anhydrase (EP4649146)|Root-specific expression of carbonic anhydrase increases the environmental carbon sequestration ability of plants. Here, a plant is genetically engineered so that its heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment. These genetically altered plants demonstrate increased levels of carbonic anhydrase activity in the extracellular environment of the plant roots, which enhances carbon sequestration in extracellular environments such as soil. WELLD BIOSCIENCES|WILD BIOSCIENCE (EP4649146)|Wild Bioscience Ltd ([GB])|(WO2024/149976)|WILD BIOSCIENCE LTD ([GB])||(CN120548358)|WELLD BIOSCIENCES, INC. ([GB])|(BR112025014035)|LTD WILD BIOSCIENCE ([GB])||(IN202517071665)|WILD BIOSCIENCE LTD|(AU2024206960)|WILD BIOSCIENCE LTD|(AR131571)|WILD BIOSCIENCE LTD.|(CA3279193)|WILD BIOSCIENCE LTD ([GB]) HENDRON ROSS|KELLY STEVEN|COSTELLO RONA (EP4649146)|HENDRON, Ross|KELLY, Steven|COSTELLO, Rona (EP4649146)|Impact Intellectual Property LLP ([GB])|Reg. Nb: 101929181|(WO2024/149976)|ICELY, Dominic ([GB])|(JP2026504057)|MURAYAMA YASUHIKO|Reg. Nb: 100108453|IIDA MASAHITO|Reg. Nb: 100188558|JITSUHIRO SHINYA|Reg. Nb: 100110364|(CN120548358)|CHENG MIAO;CHENG & PENG INTELLECTUAL PROPERTY LAW OFFICE|Reg. Nb: 11436|TANG LI;CHENG & PENG INTELLECTUAL PROPERTY LAW OFFICE|Reg. Nb: 11436|(AU2024206960)|Spruson & Ferguson ([AU])|(CA3279193)|SMART & BIGGAR LP ([CA])|Reg. Nb: 9975a484-2887-4ac6-98ad-669ac5f8e9dd (WO2024/149976)|A need exists in the art to find ways to accelerate long-term CO2 sequestration by utilising bioremediation methods. Moreover, there is a need to achieve this through scalable methods that can be implemented rapidly and globally to urgently address the issue of anthropogenic CO2 release and elevated atmospheric CO2 concentration.|Bioremediation methods, such as that presented by the present invention, have particular advantages.|In some embodiments this incorporation is stable and heritable so as to permit introduction of the modification into particular lines of crop plants; advantageously for the purposes of crop improvement or breeding programmes.|Additionally, in some embodiments the carbonic anhydrase may be attached to the outside of the cell or to the plasma membrane by a transmembrane domain, or a transmembrane helix, or a membrane anchor, or a glycosylphosphatidylinositol (GPI) anchor, or any other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell.|Additionally, these biological methods do not produce hazardous waste as byproducts, and therefore do not require expensive specialist waste disposal.|Optionally, the N-terminus or C-terminus may be fused to a transmembrane domain, transmembrane helix, or a glycosylphosphatidylinositol (GPI) anchor, or other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. The present invention also demonstrates that carbonic anhydrase proteins in various compositional forms described above can be expressed in plants using a variety of promoters that achieve the desired expression in root tissue.| (WO2024/149976)|1. A plant whose heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment.|4. A polynucleotide sequence comprising a sequence coding for a polypeptide sequence under the control of a suitable promoter, wherein the polypeptide sequence comprises a carbonic anhydrase sequence and a signal peptide sequence, wherein the promoter is active in plant roots and capable of driving overexpression of the carbonic anhydrase, the signal peptide sequence being capable of directing transport of the carbonic anhydrase into the extracellular environment of a plant root.|25. A method for increasing the capacity of a plant to sequester carbon in the soil, the method comprising altering the heritable genetic material of the plant such that a carbonic anhydrase protein is transported from the roots of the plant into the extracellular environment.| (WO2024/149976)|The invention further concerns parts of such modified plants, such as plant cells, plant parts, plant organs, fruits, seeds, embryos, germplasm and processed plant products.|The present invention provides a plant which comprises, or whose heritable genetic material comprises, a gene encoding a secretable/transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is secreted/transported from the roots of the plant into the extracellular environment. Therefore, the invention provides a plant in which the genetic material has been modified, the modification being such that the modified plants express carbonic anhydrase or a portion thereof, in at least some root cells of the plant.|The present invention relates to the field of biotechnology, and more specifically to compositions and methods for enhancing sequestration of atmospheric CO2 in soils using plants.| (WO2024/149976)|CARBONIC ANHYDRASE(100,188)|PLANT(100,155)|GROUND(100,49)|GENETIC MATERIAL(100,39)|HERITABLE GENETIC MATERIAL(100,38)|TRANSPORTABLE CARBONIC ANHYDRASE PROTEIN(100,24)|POLYNUCLEOTIDE SEQUENCE(100,23)|TRANSGENIC PLANT(100,13)|CARBON SEQUESTRATION(100,9)|SEQUESTER CARBON(100,4)|CARBONIC ANHYDRASE PROTEIN(80,54)|CARBONIC ANHYDRASE DIRECTING TRANSPORT(48,4)|ANTHROPOGENIC CO2 RELEASE ISSUE(46,1)|TRANSMEMBRANE HELIX(45,4)|ATMOSPHERIC CO2 ENHANCING SEQUESTRATION(42,1)|TRANSMEMBRANE DOMAIN(40,21)|EXPRESS CARBONIC ANHYDRASE(40,1)|ANTHROPOGENIC CO2 RELEASE(39,1)|PEPTIDE SEQUENCE(38,33)|ENHANCING SEQUESTRATION(38,1)|POLYPEPTIDE SEQUENCE(33,17)|EXPENSIVE SPECIALIST WASTE DISPOSAL(33,1)|VACUOLAR SORTING PROTEIN(31,3)|EXTRACELLULAR ENVIRONMENT(30,60)|DIRECTING TRANSPORT(30,6)|SIGNAL PEPTIDE SEQUENCE(29,31)|GLYCOSYLPHOSPHATIDYLINOSITOL(28,6)|CARBONIC ANHYDRASE SEQUENCE(27,9)|CONTICRIBRA WEISSFLOGII CARBONIC ANHYDRASE(26,6)|PLANT PROTOPLAST(26,5)|ELEVATED ATMOSPHERIC CO2(24,1)|BIOREMEDIATION(23,4)|MEMBRANE ANCHORING(23,2)|PRAIRIE GRASS(22,3)|PLANT MODIFICATION(21,4)|EXTENSIN PROTEIN(21,3)|CARBONIC ANHYDRASE TRANSPORT(20,6)|BIOMOLECULE(20,5)|BREEDING PROGRAM(20,1)|ROOT EPIDERMIS(19,2)|SECRETION(18,5)|CARROT PLANT(18,3)|PROCESSING PLANT PRODUCTION(18,3)|GERMPLASM(18,1)|INCORPORATION(18,1)|PLANT CARBON SEQUESTRATION ABILITY(18,1)|ROOT TISSUE(17,4)|PROTEIN SECRETION PATHWAY(17,3)|BYPRODUCT(17,1)|ROOT CELL(16,58)|PROGENY(16,10)|EMBRYO(16,8)|CROP(16,4)|LEVINGTON ADVANCE F2S SEED(16,4)|PROMOTOR(16,4)|MEMBRANE ANCHORING SEQUENCE(16,3)|POLYPEPTIDE CODING DNA(16,3)|PLASMA MEMBRANE(15,22)|AGROBACTERIUM TUMEFASCIEN(15,5)|PLANT ROOT(14,42)|CO2 SEQUESTRATION(14,7)|PLANT ORGAN(14,7)|LEVINGTON M3 COMPOST(14,3)|HAZARDOUS WASTE(14,1)|ATMOSPHERIC CO2(13,10)|CODING SEQUENCE(13,9)|ANCHOR(13,7)|HERITABLE GENETIC MATERIAL ALTERING(13,6)|WASTE DISPOSAL(13,1)|PLANT CELL(12,28)|SEED(12,11)|CARBONIC ANHYDRASE ACTIVITY PROTEIN(12,7)|AGROBACTERIUM LB(11,6)|POLLEN GRAIN(11,6)|SECRET ABLE TRANSPORTABLE CARBONIC ANHYDRASE(11,5)|MICROPARTICLE(11,4)|ENDOGENOUS BASELINE EXPRESSION(11,3)|SOILS(11,2)|DIATOM CONTICRIBRA WEISSFLOGII(11,1)|TRANSMEMBRANE SEQUENCE(10,7)|TREE(10,7)|EUCALYPTUS(10,3)|FRUIT(10,3)|MELCOURT SHARP SAND(10,3)|MELCOURT TOPSOIL(10,3)|PLANT TISSUE(9,12)|CARBONIC ANHYDRASE ENZYMATIC ACTIVITY(9,6)|CARBONIC ANHYDRASE ENDOGENOUS LEVEL(9,4)|CROP PLANT(9,4)|EXPERIMENTALLY CHARACTERIZED SIGNAL PEPTIDE(9,4)|REPRESENTATIVE WORDING(9,4)|SAND COMPOST(9,4)|SECRETED PROTEIN(9,4)|ALFALFA(9,3)|CELL CULTURE(9,3)|CLOVER(9,3)|MILLET(9,3)|MIRACLE GRO(9,3)|POPLAR(9,3)|SPRUCE(9,3)|SWEET POTATO(9,3)|GASEOUS CO2 INTERCONVERSION(9,2)|MATURE PLANT COMPOST(9,2)|FUNGUS ASPERGILLUS FICUUM(9,1)|GUS HISTOCHEMICAL STAINING(9,1)|HIGHLIGHT CYTOPLASMIC GFP EXPRESSION(9,1)|LONG TERM CO2 SEQUESTRATION(9,1)|RICE PLANT(9,1)|CO2 CONVERSION(8,7)|BICARBONATE ION(8,5)|HYDROPONIC BOX(8,5)|SOYBEAN PLANT ENGINEER(8,5)|CARBONIC ANHYDRASE INCREASED LEVEL(8,2)|CARBONIC ANHYDRASE SUBTYPE(8,2)|ENDOGENOUS CARBONIC ANHYDRASE(8,2)|PROCESSED PRODUCT(8,2)|ROOT SPECIFIC EXPRESSION(8,1)|SECRETED SOYBEAN CARBONIC ANHYDRASE(8,1)|HYDROPONIC SOLUTION(7,6)|ROOT CELL PROMOTER(7,6)|PERCENTAGE IDENTITY(7,4)|ATMOSPHERIC CO2 SEQUESTRATION(7,3)|BARLEY(7,3)|CALLUS CULTURE(7,3)|CANOLA(7,3)|CORN(7,3)|COTTON(7,3)|CRESS(7,3)|EXTRACELLULAR ENVIRONMENT CARBONIC ANHYDRASE(7,3)|GENE EXPRESSION REGULATORY ELEMENT(7,3)|GUS EXPRESSION(7,3)|NUCLEIC ACID SEQUENCE DETECTION(7,3)|PEA PLANT(7,3)|PINE(7,3)|SUGAR BEET(7,3)|TEFF(7,3)|TOMATO(7,3)|VETCH(7,3)|WHEAT(7,3)|DRIVING OVER EXPRESSION(7,2)|ICE CHILLED CO2(7,2)|MODIFIED CARBONIC ANHYDRASE(7,2)|PLANT SELECTABLE MARKER(7,2)|SECRET ABLE CARBONIC ANHYDRASE(7,2)|SECRETED TRANSPORTED CARBONIC ANHYDRASE(7,2)|AGROBACTERIUM TUMEFACIENS MEDIATED TRANSFORMATION(7,1)|CARBONIC ANHYDRASE ENDOGENOUS EXPRESSION(7,1)|ENGINEERED ARABIDOPSIS THALIANA PLANT(7,1)|EXTRACELLULAR ROOT CARBONIC ANHYDRASE(7,1)|MICROALGAE THALASSIOSIRA PSEUDONANA(7,1)|STAINED ARABIDOPSIS THALIANA ROOT(7,1)|TAGGED CARBONIC ANHYDRASE PROTEIN(7,1)|CRISPR(6,8)|TAILED STUDENT T TEST(6,8)|UNEQUAL VARIANCE(6,8)|AZYGOUS CONTROL PLANT(6,7)|CA PROTEIN(6,5)|DNA POLYNUCLEOTIDE SEQUENCE(6,4)|FRAGMENT FUNCTION(6,4)|ROOT EXTRACELLULAR ENVIRONMENT(6,4)|CONTAINED ENGINEERED PLANT(6,3)|EXPRESSION DOMAIN(6,3)|GLYCINE MAX(6,3)|GROUND BIOMASS(6,3)|RYE(6,3)|ARABIDOPSIS ROOT(6,2)|AZYGOUS PLANT(6,2)|COLORIMETRIC ASSAY(6,2)|CONCENTRATED HYDROPONIC MEDIA SAMPLE(6,2)|EXTRACELLULAR MEMBRANE(6,2)|EXTRACELLULAR ROOT ENVIRONMENT(6,2)|GENE REPORTER FUSION(6,2)|MULTICLONING SITE(6,2)|PERLITE SOIL(6,2)|SEQUESTERING CO2(6,2)|TARGETING PEPTIDE(6,2)|TRANSGENIC MANIPULATION(6,2)|TRANSPORT CARBONIC ANHYDRASE(6,2)|UNTRANSFORMED PLANT(6,2)|BACTERIAL SELECTABLE MARKER(6,1)|CARBONIC ANHYDRASE ESTERASE(6,1)|CARBONIC ANHYDRASE POLYPEPTIDE(6,1)|CARROT EXTENSIN(6,1)|CLEAR CYTOSOLIC LOCALIZATION(6,1)|CO2 SOIL FLUX EXPERIMENT(6,1)|DONOR REPAIR TEMPLATE(6,1)|ENGINEERED CARBONIC ANHYDRASE(6,1)|ENGINEERED SOYBEAN HAIRY ROOT(6,1)|EUKARYOTIC CARBONIC ANHYDRASE(6,1)|EXOGENOUS POLYNUCLEOTIDE(6,1)|EXTRACELLULAR CARBONIC ANHYDRASE(6,1)|EXTRACELLULAR CO2 HYDRATION(6,1)|FUSION CARBONIC ANHYDRASE PROTEIN(6,1)|GUS STAINED ROOT(6,1)|HARNESSING CARBONIC ANHYDRASE(6,1)|INTRACELLULAR CARBONIC ANHYDRASE(6,1)|JOHN INNES CEREAL MIX(6,1)|ORGANISM SKELETAL TISSUE(6,1)|POLYNUCLEOTIDE CARBONIC ANHYDRASE(6,1)|POSITIVELY TRANSFORMED ROOT TISSUE(6,1)|PROTEIN NONCONVENTIONAL TRANSPORT(6,1)|RADIO TRACER ASSAY(6,1)|SOYBEAN EXPANSIN GENE PROMOTER(6,1)|SOYBEAN PROTOPLAST CONFOCAL IMAGE(6,1)|SOYBEAN PROTOPLAST PLASMA MEMBRANE(6,1)|TRANSFECTED PROTOPLAST(6,1)|TRANSFORMED PLANT REGENERATION(6,1)|VISUAL REPORTER EXPRESSION(6,1)|ELECTROPORATION(5,6)|GENETICALLY ENGINEERED PLANT(5,6)|N TERMINUS(5,6)|CELL WALL(5,5)|HOMOLOGY(5,5)|BIOMASS PRODUCTION(5,3)|DIRECTING SECRETION TRANSPORT(5,3)|MEASURABLE DECREASE(5,3)|ORDINARY SKILL PERSON(5,3)|POSITIVE COLONY(5,3)|SHOW CARBONIC ANHYDRASE(5,3)|SOIL INORGANIC CARBON CONTENT(5,3)|DIAMETER SOIL SAMPLER PROBE(5,2)|ENGINEERED PLANT ROOT(5,2)|ENHANCE CO2 SEQUESTRATION(5,2)|GROWTH PHENOTYPE(5,2)|ME AGAR(5,2)|RECOMBINATION SITE(5,2)|RI PLASMID(5,2)|SOIL SLURRY(5,2)|SYNTHETIC PROMOTER(5,2)|AEROPONIC GROWTH(5,1)|AGROBACTERIUM RHIZOGENE STRAIN(5,1)|AGROBACTERIUM STRAIN(5,1)|CARBONIC ANHYDRASE ASSAY(5,1)|CARBONIC ANHYDRASE DRIVING EXPRESSION(5,1)|CARBONIC ANHYDRASE MRNA(5,1)|CARBONIC ANHYDRASE VARIANT(5,1)|CHILLED PESTLE(5,1)|DIFFERING POLYNUCLEOTIDE PEPTIDE SEQUENCE(5,1)|ENCODED CARBONIC ANHYDRASE(5,1)|EXTRACTION BUFFER OOPI(5,1)|GENETICALLY ENGINEERED ARABIDOPSIS(5,1)|GRAM NEGATIVE BACTERIUM BURKHOLDERIA(5,1)|GUS STAINING BUFFER(5,1)|HIGHLIGHT FLUORESCENT PROTEIN EXPRESSION(5,1)|HOMOGENIZED ROOT SAMPLE(5,1)|INDUCIBLE PROMOTER(5,1)|INTERESTING OPPORTUNITY(5,1)|LYSOSOMAL SECRETION(5,1)|METLER PH PROBE(5,1)|MICROALGAE SPECIES(5,1)|MONOMERIC SUBTYPE(5,1)|NATIVE CARBONIC ANHYDRASE SEQUENCE(5,1)|NONENGINEERED PLANT(5,1)|OOPI EXTRACTION BUFFER(5,1)|POLYSACCHARIDE ANCHOR(5,1)|SEA URCHIN LARVA(5,1)|SEQUESTRATION MAGNITUDE(5,1)|SIGNALING PEPTIDE(5,1)|SOYBEAN ROOT HAIR(5,1)|UNCONVENTIONAL SECRETORY PATHWAY(5,1)|WILDTYPE ROOT ENVIRONMENT(5,1)|WORD CARBONIC ANHYDRASE(5,1)|Y CARBONIC ANHYDRASE(5,1)|COVER CROP(4,7)|PLANT TRANSFORMATION VECTOR(4,7)|ABSORBANCE(4,4)|PROTON(4,4)|SPECTINOMYCIN(4,4)|SUPERNATANT(4,4)|GLYCOPROTEIN(4,3)|OIL PALM(4,3)|BASELINE COMPARISON(4,2)|CELL STRAINER(4,2)|CO2 TURN CATALYZED CONVERSION(4,2)|DISCERNIBLE DIFFERENCE(4,2)|HYDROPONIC MEDIUM SAMPLE(4,2)|MEMBRANE BOUND PROTEIN(4,2)|PLANT CELL GENOME(4,2)|RECORDING WINDOW(4,2)|WASHING(4,2)|CARBONIC ANHYDRASE DETECTION(4,1)|CARBONIC ANHYDRASE PROTEIN PRODUCTION(4,1)|CARBONIC ANHYDRASE SECRETION TRANSPORT(4,1)|CASTOR BEAN CATALASE(4,1)|CELLULAR EXPORT(4,1)|CLONAL PROPAGATION(4,1)|CO2 SEQUESTRATION FACILITATION(4,1)|CO2 SEQUESTRATION MEDIATION(4,1)|EXCESS HYDROPONIC MEDIA(4,1)|EXOGENOUS SOIL TREATMENT(4,1)|EXTRACELLULAR EXPRESSION(4,1)|EXTRACORPOREAL CO2 REMOVAL(4,1)|FLORAL DIPPING(4,1)|GENETICALLY ENGINEERED SOYBEAN ROOT(4,1)|HAIRY ROOT TRANSFORMATION(4,1)|HCO3 ENHANCED CONVERSION(4,1)|HORTICULTURAL PLANT(4,1)|HYDROPONIC GROWTH ENVIRONMENT(4,1)|LEADER PEPTIDE(4,1)|MEAN CARBONIC ANHYDRASE(4,1)|MITIGATE SOIL EROSION(4,1)|MWCO PROTEIN(4,1)|NA2EDTA H2O(4,1)|ONEVIEW CAMERA(4,1)|PLANT NODULE(4,1)|PRIME EDITING(4,1)|PROMOTER GUS FUSION(4,1)|PROTEIN CONCENTRATION(4,1)|PROTEIN SECRETORY PATHWAY(4,1)|RELEASING ENZYME(4,1)|REPORTER GENE FUSION(4,1)|SEEDLING ROOT(4,1)|SEMIAQUATIC PLANT(4,1)|SOIL GROWN PLANT(4,1)|SORGHUM RICE(4,1)|SOYBEAN TRANSFORMATION(4,1)|TARGETED NUCLEASE(4,1)|TRANSGENIC ROOT SAMPLE(4,1)|TRANSGENIC SOYBEAN PLANT(4,1)|TRANSIT PEPTIDE(4,1)|VIRAL TRANSFECTION(4,1)|WEED PEST MANAGEMENT(4,1)|HERBICIDE RESISTANCE(3,6)|GRNA(3,5)|SEQUENCE IDENTITY(3,5)|ACETONITRILE(3,3)|BIOFUEL(3,3)|CULTIVAR(3,3)|DAUCUS CAROTA(3,3)|ENHANCER(3,3)|FALLOW PERIOD(3,3)|GENETIC ENGINEERING(3,3)|INTERNAL ENVIRONMENT(3,3)|PISUM SATIVUM(3,3)|SPECTROPHOTOMETER PLATE READER(3,3)|TERMINATOR(3,3)|ARABLE LAND(3,2)|ASEXUAL REPRODUCTION(3,2)|BROMOTHYMOL BLUE(3,2)|CASSAVA VEIN MOSAIC VIRUS(3,2)|CONVERSION ENHANCEMENT(3,2)|EQUILIBRIUM(3,2)|FLOWERING(3,2)|FORESTRY(3,2)|INCREASED ACCUMULATION(3,2)|INCREASED CARBONIC ANHYDRASE(3,2)|INORGANIC SOIL CARBON(3,2)|KANAMYCIN(3,2)|MICROINJECTION(3,2)|P NITROPHENYL HYDROLYSIS(3,2)|PLANT PRODUCTION(3,2)|SAMPLE FILTRATION(3,2)|SOIL RESPIRATION(3,2)|TALE NUCLEASE(3,2)|TUBER(3,2)|ABSORPTION COMPOUND(3,1)|ACTIVE ENGINEERED PLANT(3,1)|AGROECOSYSTEM(3,1)|ANCESTOR CELL(3,1)|ANCHOR MOLECULE(3,1)|ANIMAL CONSUMPTION(3,1)|BACKWARD REACTION(3,1)|BICARBONATE SALT(3,1)|BRASSICA OLERACEA(3,1)|CA NUCLEASE(3,1)|CALLUS TISSUE(3,1)|CARBONIC ANHYDRASE ADAPTATION(3,1)|CARBONIC ANHYDRASE CODING SEQUENCE(3,1)|CARBONIC ANHYDRASE ENZYME ACTIVITY(3,1)|CARBONIC ANHYDRASE INCREASED EXPRESSION(3,1)|CARBONIC ANHYDRASE SOLUTION(3,1)|CHOICE SPECIES(3,1)|CO2 DISSOLUTION(3,1)|CO2 ENHANCED CONVERSION(3,1)|CONFERRED GENE EXPRESSION(3,1)|CONTRIBUTOR(3,1)|CROP PLANT SPECIES(3,1)|CRUSHED ROCK SOIL TREATMENT(3,1)|CYTOPLASMIC LOCALIZED CONTROL(3,1)|DOUBLE STRANDED BREAK(3,1)|DRIED BIOMASS(3,1)|ENHANCED CO2 SEQUESTRATION(3,1)|ENTIRE GLYCOPHOSPHATIDYLINOSITOL(3,1)|ENZYME ACTIVITY ASSAY(3,1)|ENZYME DISTRIBUTION(3,1)|ENZYME SEQUENCE(3,1)|EX VIVO EX PLANT(3,1)|EXOSOME RELEASE(3,1)|EXPRESSION ENHANCEMENT(3,1)|FERTILIZER TREATMENT(3,1)|GASEOUS CARBON DIOXIDE INTERCONVERSION(3,1)|GENE EDITING PROTEIN(3,1)|GENETICALLY ENGINEERED SOYBEAN PLANT(3,1)|GENETICALLY ENHANCED PLANT(3,1)|GRAMNEGATIVE BACTERIA(3,1)|HARVEST ABLE SEED(3,1)|HOST GENOME(3,1)|HYDROPONIC CONDITION(3,1)|IMMEDIATE ENVIRONMENT(3,1)|INORGANIC CARBON SEQUESTRATION(3,1)|INORGANIC ION(3,1)|ISOLATED PROTEIN SAMPLE(3,1)|LIFE DOMAIN(3,1)|LOCALIZATION SEQUENCE(3,1)|MERISTEMATIC REGION(3,1)|MULTIMER FORMATION(3,1)|NATIVE REGULATORY SEQUENCE(3,1)|NATURALLY OCCURRING ENZYME(3,1)|NATURALLY OCCURRING PROMOTER(3,1)|NET CARBON SEQUESTRATION(3,1)|NUTRIENT CONTENT(3,1)|OBSERVABLE NEGATIVE(3,1)|PGMPIN2B PROMOTER CONTROL(3,1)|PLANT EXPRESSION VECTOR(3,1)|PLANT ROOT TISSUE(3,1)|POLYNUCLEOTIDE ISOLATION(3,1)|POLYPEPTIDE ISOLATION(3,1)|PRIMARY MESENCHYME CELL CALCIFICATION(3,1)|PROTEIN CONSTRUCT(3,1)|PROTOCOL ADAPTED VERSION(3,1)|REDUCING GLOBAL CO2 EMISSION(3,1)|RNA COATED PARTICLE BOMBARDMENT(3,1)|ROOT PROMOTER SEQUENCE(3,1)|ROOT SPECIFIC PROMOTER VARIANT(3,1)|ROOTSPECIFIC CELL(3,1)|SEA FLOOR(3,1)|SNAP LID MICROCENTRIFUGE TUBE(3,1)|SOIL CO2 SEQUESTRATION RATE(3,1)|SOIL PH TESTER(3,1)|SOYBEAN ROOT CELL(3,1)|STABLE TRANSFORMATION(3,1)|SUBCELLULAR LOCALIZATION(3,1)|TARGET PEPTIDE(3,1)|TARGET PLANT(3,1)|TEMPLATE SEQUENCE(3,1)|TERRESTRIAL ECOSYSTEM(3,1)|THALASSIOSIRA WEISSFLOGII(3,1)|UNMODIFIED PLANT(3,1)|UNQUALIFIED SENSE(3,1)|VEGETATIVE CYCLE(3,1)|WATER REVERSIBLE CONVERSION(3,1)|Y SUBTYPE(3,1)|WILD TYPE PLANT(2,10)|CARBONIC ANHYDRASE EXPRESSION(2,4)|FIVE FOLD(2,3)|LBA(2,3)|PLANT FOOD(2,3)|NONHOMOLOGOUS END JOINING REPAIR(2,2)|ACCESSION NUMBER GLYMA 19G(2,1)|ACCLIMATIZATION(2,1)|ADZUKI BEAN(2,1)|ANCHORAGE(2,1)|APOPTOSIS(2,1)|AQUEOUS ENVIRONMENT(2,1)|ARABLE FARMING(2,1)|ARCHAEA(2,1)|AVERAGE SKILL(2,1)|BASE EDITOR(2,1)|BASE SUBSTITUTION(2,1)|BETA GLUCURONIDASE(2,1)|BIOCHEMISTRY(2,1)|BIODIVERSITY(2,1)|BIOINFORMATICS(2,1)|BIOLISTIC(2,1)|BLEBBING(2,1)|BOTANY(2,1)|BROMOCRESOL PURPLE(2,1)|C4 PHOTOSYNTHESIS(2,1)|CARBONIC ANHYDRASE LEVEL(2,1)|CELL EXTRACELLULAR ENVIRONMENT(2,1)|CELL TARGET PROTEIN(2,1)|CHAMBER COVER(2,1)|CHLOROPHYL(2,1)|COLOR CHANGE(2,1)|COMBINED EFFORT(2,1)|CONFOCAL MICROSCOPE(2,1)|CONTROL ARABIDOPSIS THALIANA PLANT(2,1)|CONTROLLED BREEDING(2,1)|COWPEA(2,1)||(JP2026504057)|CARBONIC ANHYDRASE(100,192)|TRANSGENIC PLANT(100,10)|CARBON SEQUESTRATION(100,6)|CARBONIC ANHYDRASE PROTEIN(99,58)|TRANSPORTABLE CARBONIC ANHYDRASE PROTEIN(83,6)|CARBONIC ANHYDRASE TRANSPORT(49,8)|AGROBACTERIUM TMEPHASIEN(48,1)|POLYPEPTIDE SEQUENCE(46,17)|EXPENSIVE PROFESSIONAL WASTE DISPOSAL(44,1)|ENHANCING(40,1)|EXTRACELLULAR ENVIRONMENT(39,60)|SUBTYPES(39,2)|CARBONIC ANHYDRASE SEQUENCE(38,9)|HARMFUL WASTE(38,1)|MODIFIED PLANT EXPRESS(38,1)|POLLEN GRANULE(37,1)|HEREDITARY GENETIC MATERIAL(31,20)|POLYNUCLEOTIDE SEQUENCE(30,25)|DESIGNATION(30,1)|PLANT ROOT(29,43)|AGROBACTERIUM SPECIES(29,2)|SIGNAL PEPTIDE SEQUENCE(28,31)|EXTENSIN PROTEIN(28,3)|PHOTOSYNTHESIS(28,1)|SUGAR RADISH(27,2)|PROTEIN SECRETION ROUTE(27,1)|PROCESSING PLANT PRODUCTION(26,7)|ROOT CELL EXPRESSION(26,1)|CARROT PLANT(25,3)|CROP(25,3)|EMBRYO(24,8)|OFFSPRING(24,7)|MEMBRANE ANCHORING SEQUENCE(24,2)|UPTAKE(24,1)|ACTIVE PROMOTER(23,8)|LEVINGTON ADVANCE F2S SEED(23,4)|ISOFORM(23,1)|ROOT CELL(22,49)|PLANT CARBON ISOLATING ABILITY(22,1)|GROUND(21,49)|PRAIRIE GLASS(21,2)|SEED(20,13)|PLANT ORGAN(20,7)|DESCENDANT(20,1)|PLANT CELL(19,26)|AGROBACTERIUM TUMEFASCIEN(19,4)|BIOREMEDIATION(19,4)|BREEDING PROGRAM(19,1)|WASTE DISPOSAL(19,1)|CARBONIC ANHYDRASE ACTIVITY PROTEIN(18,8)|COVER CROP(18,7)|PLANT MODIFICATION(18,4)|GENE EDITING(18,3)|CARBONIC ANHYDRASE OVER EXPRESSION(18,2)|HYDRATION(18,2)|PLANT ROOT EXTRACELLULAR ENVIRONMENT(18,2)|SOYBEAN EXPANSIN(17,4)|PLANT MANIPULATION(16,10)|ENDOGENOUS BASELINE EXPRESSION(16,3)|VACUOLATION(16,2)|UNEQUAL DISPERSION(15,8)|ESCHERICHIA(15,2)|SUBTYPE CARBONIC ANHYDRASE(15,2)|CONTICULIBRA WEITHOGY CARBONIC ANHYDRASE(15,1)|CONTICULIBULA WEITHOGIE CARBONIC ANHYDRASE(15,1)|SECRETED PROTEIN(15,1)|IDENTITY SEQUENCE(14,12)|TREE(14,7)|PLANT CELL TRANSFORMATION(14,4)|TRANSMEMBRANE HELIX(14,4)|EUCALYPTUS(14,3)|FRUIT(14,3)|CONTICRIBRA WEISSFLOGII CARBONIC ANHYDRASE(14,1)|DIATOMACEOUS CONTICLIBRA WEISSFLOGI(14,1)|CELL CULTURE(13,3)|POPLAR(13,3)|SWEET POTATO(13,3)|MATURE PLANT COMPOST(13,2)|GENETIC MATERIAL(12,35)|INHERITED GENETIC MATERIAL(12,12)|PLANT TISSUE(12,12)|CROP PLANT(12,4)|POLLEN GRAIN(12,4)|REPRESENTATIVE WORDING(12,4)|SAND COMPOST(12,4)|TRANSMEMBRANE DOMAIN SEQUENCE(12,4)|ALFALFA(12,3)|CLOVER(12,3)|MILLET(12,3)|ENDOGENOUS CARBONIC ANHYDRASE(12,2)|HYDROPONIC CULTIVATION(12,2)|MELCOURT SHARP SAND(12,2)|FUNGUS ASPERGILLUS FICUUM(12,1)|GROWING ARABIDOPSIS SALIANA PLANT(12,1)|MANIPULATED ARABIDOPSIS SALIANA PLANT(12,1)|MANIPULATED SOYBEAN HAIRLIKE ROOT(12,1)|RICE PLANT(12,1)|UNCLEAVED TRANSMEMBRANE DOMAIN(12,1)|HYDROPONIC BOX(11,5)|BARLEY(11,3)|BETCH(11,3)|CALLUS CULTURE(11,3)|CANOLA(11,3)|GENE EXPRESSION REGULATORY ELEMENT(11,3)|TOMATO(11,3)|PROCESSED PRODUCT(11,2)|AGROBACTERIUM THUMEFACIENSIS MEDIATED TRANSFORMATION(11,1)|EXTRACELLULAR ROOT CARBONIC ANHYDRASE(11,1)|LEVINGTON M3 COMPOST(11,1)|ROOT SPECIFIC EXPRESSION(11,1)|SECRETED SOYBEAN CARBONIC ANHYDRASE(11,1)|HYDROPONIC SOLUTION(10,6)|REGULATORY ELEMENT(10,5)|HYDROPONIC MEDIA(10,4)|PERCENTAGE IDENTITY(10,4)|COTTON(10,3)|GUS EXPRESSION(10,3)|PEA PLANT(10,3)|TEFF(10,3)|WHEAT(10,3)|CARBONIC ANHYDRASE ASSAY(10,2)|MIRACLE GRO(10,2)|SECRET ABLE TRANSPORTABLE CARBONIC ANHYDRASE(10,2)|CARBONIC ANHYDRASE ENDOGENOUS EXPRESSION(10,1)|CONTICULIBRA WEISTOCYTE CARBONIC ANHYDRASE(10,1)|STAINED ARABIDOPSIS THALIANA ROOT(10,1)|VACUOLAR SORTING PROTEIN(10,1)|PLANT ROOT CELL(9,10)|CA PROTEIN(9,5)|CARBONIC ANHYDRASE ENDOGENOUS LEVEL(9,3)|CORN(9,3)|NUCLEIC ACID SEQUENCE DETECTION(9,3)|PINE(9,3)|PROTEIN SECRETION PATHWAY(9,3)|ROW CROP(9,3)|TRANSCRIPTIONAL FACTOR(9,3)|TRISHCL PH(9,3)|ARABIDOPSIS ROOT(9,2)|CARBONIC ANHYDRASE SECRETION TRANSPORT(9,2)|COLORIMETRIC ASSAY(9,2)|EXTRACELLULAR MEMBRANE(9,2)|EXTRACELLULAR ROOT ENVIRONMENT(9,2)|MULTICLONING SITE(9,2)|MWCO PROTEIN CONCENTRATION COLUMN(9,2)|ROOT HOMOGENIZATION(9,2)|STABLE TRANSGENIC STRAIN(9,2)|UNMANIPULATED PLANT(9,2)|UNTRANSFORMED PLANT(9,2)|ABOVEGROUND BIOMASS(9,1)|AGROBACTERIUM TAMEFASCIEN(9,1)|AGROBACTERIUM TUMEFASSIEN(9,1)|BURKHOLDERIA TERRITORII(9,1)|CARBONIC ANHYDRASE PROTEIN EXPRESSION(9,1)|CONTICULIBRA WEITHOLOGY(9,1)|CYTOPLASMIC GFP EXPRESSION(9,1)|EXTRACELLULAR CARBONIC ANHYDRASE DETECTION(9,1)|ORGANISM SKELETAL TISSUE(9,1)|PROMOTER GUS FUZE(9,1)|PROTEIN NONCONVENTIONAL TRANSPORT(9,1)|SOY EXPANSIN GENE PROMOTER(9,1)|DNA POLYNUCLEOTIDE SEQUENCE(8,4)|FRAGMENT FUNCTION(8,4)|OVER EXPRESSION(8,3)|UNMODIFIED PLANT(8,2)|AGRICULTURAL ECOSYSTEM(8,1)|BAD IMPACT MITIGATION(8,1)|CARBONIC ANHYDRASE POLYPEPTIDE(8,1)|CARBONIC ANHYDRASE SUBTYPE(8,1)|CARROT EXTENSIN(8,1)|DONOR REPAIR TEMPLATE(8,1)|EXOGENOUS POLYNUCLEOTIDE(8,1)|FUZED CARBONIC ANHYDRASE PROTEIN(8,1)|GENETIC MATERIAL MODIFICATION(8,1)|GLYCOSYLPHOSPHATIDYLINOSITOL EXPRESSION(8,1)|INTRACELLULAR CARBONIC ANHYDRASE(8,1)|JOHN INNES CEREAL MIX(8,1)|MELCOURT TOPSOIL(8,1)|MONOCOTYLEDONOUS PLANT(8,1)|SECRETORY TRANSPORTABLE CARBONIC ANHYDRASE(8,1)|SOY PROTOPLAST CONFOCAL IMAGE(8,1)|SOYBEAN PROTOPLAST PLASMA MEMBRANE(8,1)|SPRUCE CATALASE(8,1)|TRANSFECTED PROTOPLAST(8,1)|TRANSFORMED PLANT REGENERATION(8,1)|UNDERGROUND BIOMASS(8,1)|VISUAL REPORTER EXPRESSION(8,1)|ELECTROPORATION(7,6)|HERBICIDE RESISTANT(7,6)|BIOMOLECULE(7,5)|BIOMASS PRODUCTION(7,3)|GENE MODIFICATION(7,3)|POSITIVE COLONY(7,3)|SOIL INORGANIC CARBON CONTENT(7,3)|CONCENTRATED HYDROPONIC MEDIUM SAMPLE(7,2)|GENETICALLY ENGINEERED SOYBEAN PLANT(7,2)|GROWTH PHENOTYPE(7,2)|ME AGAR(7,2)|RECOMBINANT SITE(7,2)|RI PLASMID(7,2)|SAMPLER PROBE(7,2)|SOIL SLURRY(7,2)|SYNTHETIC PROMOTER(7,2)|VERSION MATCH(7,2)|AGRICULTURE CULTIVATION(7,1)|AGROBACTERIUM RHIZOGENE STRAIN(7,1)|AGROBACTERIUM STRAIN(7,1)|AQUATIC PLANT(7,1)|CARBONIC ANHYDRASE COPY(7,1)|CARBONIC ANHYDRASE DOMAIN(7,1)|CARBONIC ANHYDRASE ENCODING SEQUENCE(7,1)|CARBONIC ANHYDRASE EXPRESSION PROTEIN(7,1)|CARBONIC ANHYDRASE MRNA(7,1)|CARBONIC ANHYDRASE VARIANT(7,1)|CHLOROPHYL CLEARED SEEDLING(7,1)|CLEAR CYTOSOL LOCALIZATION(7,1)|DAUCAS CAROTA(7,1)|DAUKAS CAROTA(7,1)|EQUIVALENT UNTRANSFORMED ROOT TISSUE(7,1)|GENETICALLY ENGINEERED ARABIDOPSIS(7,1)|GUS REPORTER(7,1)|INTERESTING OPPORTUNITY(7,1)|LEICA TCS(7,1)|LYSOSOMAL SECRETION(7,1)|MANIPULATED CARBONIC ANHYDRASE(7,1)|METLER PH PROBE(7,1)|MICROALGAE SPECIES(7,1)|MONOMERIC SUBTYPE(7,1)|NATIVE CARBONIC ANHYDRASE SEQUENCE(7,1)|NONCONVENTIONAL SECRETION PATH(7,1)|NONHOMOLOGOUS TERMINAL LINKAGE(7,1)|NONMANIPULATED STRAIN(7,1)|NONPLANT ORGANISM(7,1)|NONSECRETORY PATHWAY(7,1)|PNEUMONIC GROWTH(7,1)|POLYSACCHARIDE ANCHOR(7,1)|PRAIRIE GRASS(7,1)|PROTEIN REARRANGEMENT(7,1)|RELIABLY TRANSFORMED ROOT TISSUE(7,1)|RETAINING CARBONIC ANHYDRASE(7,1)|SEA URCHIN LARVA(7,1)|SECRET ABLE CARBONIC ANHYDRASE(7,1)|SECRETED TRANSPORTED CARBONIC ANHYDRASE(7,1)|SOIL ECOSYSTEM(7,1)|SOYBEAN ROOT HAIR(7,1)|TALE NUCLEASE(7,1)|TARGETED NUCLEASE(7,1)|STANDARD ERROR BAR(6,9)|GENETICALLY MODIFIED PLANT(6,6)|ABSORBANCE(6,4)|GENETICALLY ENGINEERED PLANT(6,4)|HOMOLOGY(6,4)|P NITROPHENYL HYDROLYSIS(6,4)|SPECTINOMYCIN(6,4)|SUPERNATANT(6,4)|FALLOW PERIOD(6,3)|FINE PARTICLE(6,3)|GLYCOPROTEIN(6,3)|OIL PALM(6,3)|CELL STRAINER(6,2)|DIRECTING SECRETION TRANSPORT(6,2)|DISCERNIBLE DIFFERENCE(6,2)|GENE REPORTER FUSION PRODUCT(6,2)|INTERNATIONAL RELEASE(6,2)|MANIPULATED PLANT ROOT(6,2)|MEASURABLE DECREASE(6,2)|MEMBRANE BOUND PROTEIN(6,2)|MODIFIED CARBONIC ANHYDRASE(6,2)|SHOW CARBONIC ANHYDRASE(6,2)|STABLE STRAIN(6,2)|TRISHCL SOLUTION(6,2)|ACCELERATE ROCK(6,1)|ANCESTRAL CELL(6,1)|CARBONIC ANHYDRASE ABSENCE(6,1)|CARBONIC ANHYDRASE INDUCTION(6,1)|CARBONIC ANHYDRASE PROTEIN PRODUCTION(6,1)|CELLULAR LOCALIZATION(6,1)|CLONAL REPRODUCTION(6,1)|CREEP(6,1)|DICOTYLEDONOUS PLANT(6,1)|EXTRACELLULAR EXPRESSION(6,1)|FLORAL DIPPING(6,1)|HCO ENHANCED CONVERSION(6,1)|HOMOGENIZED ROOT SAMPLE(6,1)|HORTICULTURAL PLANT(6,1)|HYDROPONIC GROWTH ENVIRONMENT(6,1)|INDUCING PROMOTER(6,1)|MEAN CARBONIC ANHYDRASE(6,1)|MITIGATE SOIL EROSION(6,1)|ONEVIEW CAMERA(6,1)|PEARLITE SOIL(6,1)|PLANT PROTOPLAST(6,1)|POLYNUCLEOTIDE ISOLATION(6,1)|PRIME EDITING(6,1)|REPORTER GENE FUSION(6,1)|RNA COATED MICROPARTICLE GUN(6,1)|ROOT EPIDERMIS CELL(6,1)|ROOT PROMOTER(6,1)|SECRETORY VERSION(6,1)|SOIL INORGANIC CARBON ACCUMULATION(6,1)|SORGHUM RICE(6,1)|SOYBEAN TRANSFORMATION(6,1)|SPECIES POLYPEPTIDE SEQUENCE(6,1)|SUGAR DAIKON(6,1)|TRANSGENIC MANIPULATION(6,1)|TRANSGENIC ROOT SAMPLE(6,1)|TRANSGENIC SOYBEAN PLANT(6,1)|TRANSMEMBRANE SEQUENCE VARIANT(6,1)|TRANSPORT CARBONIC ANHYDRASE(6,1)|VIRAL TRANSFECTION(6,1)|PLANT TRANSFORMATION VECTOR(5,7)|ACETONITRILE(5,3)|BIOFUEL(5,3)|ENHANCER(5,3)|EXPERIMENTALLY CHARACTERIZED SIGNAL PEPTIDE(5,3)|PISUM SATIVUM(5,3)|SECRETORY PROTEIN(5,3)|SPECTROPHOTOMETER PLATE READER(5,3)|TERMINATOR(5,3)|PLANT CELL GENOME(5,2)|ARBITRARY ENZYME(5,1)|ARBITRARY SPECIES(5,1)|CA NUCLEASE(5,1)|CALLUS TISSUE(5,1)|COOLED MAMMALIAN BAR(5,1)|DNA INJECTION(5,1)|DRIED BIOMASS(5,1)|ENZYME DISTRIBUTION(5,1)|EX VIVO EX PLANT(5,1)|EXOSOMAL RELEASE(5,1)|EXTRACELLULAR CARBONIC ANHYDRASE LEVEL(5,1)|EXTRINSIC SOIL PROCESSING(5,1)|FLUORESCENT PROTEIN EXPRESSION(5,1)|GASEOUS CARBON DIOXIDE INTERCONVERSION(5,1)|GENE EDITING PROTEIN(5,1)|GENE VECTOR(5,1)|GLYCOPHOSPHATIDYLINOSITOL(5,1)|GUS STAINED ROOT REGION(5,1)|HAIR ROOT TRANSFORMATION(5,1)|HARVEST ABLE SEED(5,1)|HOMOLOGOUS DIRECTED REPAIR(5,1)|HOST GENOME(5,1)|ISOLATED PROTEIN SAMPLE(5,1)|JAPANESE PAMPAS GRASS(5,1)|OBSERVABLE NEGATIVE(5,1)|OPERATED PLANT ROOT(5,1)|POLLEN PARTICLE(5,1)|POLYPEPTIDE ISOLATION(5,1)|PRIMARY CALCIFIED MESENCHYMAL CELL(5,1)|PROMOTER EXPRESSION REGION(5,1)|SEA FLOOR(5,1)|SEMISOLID PLANT(5,1)|SILICATE ROCK(5,1)|SLAKED LIME CA(5,1)|SOY ROOT(5,1)|TARGET PLANT(5,1)|TRANSGENIC PLANT ROOT ENVIRONMENT(5,1)|TRIS HCL PH(5,1)|UNLIMITED SENSE(5,1)|VEGETATIVE CYCLE(5,1)|GPI(4,5)|GRNA(4,5)|SEQUENCE IDENTITY(4,5)|PROTON(4,4)|WILD PLANT(4,4)|INTERNAL ENVIRONMENT(4,3)|ARABLE LAND(4,2)|ASEXUAL REPRODUCTION(4,2)|BROMOTHYMOL BLUE(4,2)|CASSAVA VEIN MOSAIC VIRUS(4,2)|CM DIAMETER LAND(4,2)|EQUILIBRIUM(4,2)|EQUIVALENCE(4,2)|FLOWERING(4,2)|FORESTRY(4,2)|FUSION PRODUCTION(4,2)|GENETICALLY MODIFIED SOYBEAN PLANT(4,2)|GROWING CONTROLLED SOYBEAN PLANT(4,2)|KANAMYCIN(4,2)|MICROINJECTION(4,2)|MORPHOLOGY(4,2)|MULASHIGESCOOG(4,2)|NONMANIPULATED CONTROL PLANT(4,2)|PHOTOGRAPH(4,2)|PLANT SELECTION MARKER(4,2)|REVERSE REACTION(4,2)|SAMPLE FILTRATION(4,2)|SOIL CARBON CHECK(4,2)|SOIL RESPIRATION(4,2)|TUBER(4,2)|ACCLIMATIZATION(4,1)|ADJACENT AGROBACTERIUM LB(4,1)|AGROBACTERIUM TUMEFACIENS(4,1)|ALONE PLANT(4,1)|ANCHOR MOLECULE(4,1)|ARBITRARY CELL(4,1)|ARBITRARY POLYNUCLEOTIDE SEQUENCE(4,1)|BACTERIAL SELECTION MARKER(4,1)|BED MEDIUM(4,1)|BICARBONATE FORMATION(4,1)|BICARBONATE SALT(4,1)|BIOREVITALIZATION(4,1)|BRASSICA OLERACEA(4,1)|CARBONIC ANHYDRASE INCREASED EXPRESSION(4,1)|CARBONIC ANHYDRASE SOLUTION(4,1)|CELL EXPORT(4,1)|CLEAR PHENOTYPIC DIFFERENCE(4,1)|CONVERSION ENHANCEMENT(4,1)|CRISPR ACTION(4,1)|CROP PLANT SPECIES(4,1)|DIRECTING TRANSPORT(4,1)|DOUBLE STRANDED CLEAVAGE(4,1)|ENHANCED CARBON ISOLATION(4,1)|ENZYME ACTIVITY ASSAY(4,1)|ENZYME RELEASE(4,1)|ENZYME SEQUENCE(4,1)|EXCESS HYDROPONIC MEDIUM(4,1)|EXPRESSION ENHANCEMENT(4,1)|EXTRACT BUFFER(4,1)|GENE EDITING TOOL(4,1)|GENETICALLY ENHANCED PLANT(4,1)|GRAMNEGATIVE BACTERIA(4,1)|GUS STAINING BUFFER SOLUTION(4,1)|HYDROPONIC CONDITION(4,1)|HYDROPONIC CULTURE MEDIUM(4,1)|INORGANIC CARBON SEQUESTRATION(4,1)|LIFE DOMAIN(4,1)|LOCALIZING SEQUENCE(4,1)|MEASURABLE REDUCTION(4,1)|MULTIMER FORMATION(4,1)|NATIVE REGULATORY SEQUENCE(4,1)|NATURALLY OCCURRING PROMOTER(4,1)|NET CARBON SEQUESTRATION(4,1)|NUTRIENT CONTENT(4,1)|NUTRIENT STORAGE(4,1)|PLANT EXPRESSION VECTOR(4,1)|PLANT ROOT GRAIN(4,1)|PLANT ROOT TISSUE(4,1)|PRODUCED CARBONIC ANHYDRASE PROTEIN(4,1)|RECORDING WINDOW(4,1)|SOIL GROWING PLANT(4,1)|SOIL PH TESTER(4,1)|SOYBEAN ROOT CELL(4,1)|STABLE TRANSFORMATION(4,1)|TARGET PEPTIDE SEQUENCE(4,1)|TEMPLATE SEQUENCE(4,1)|THALASSIOSIRA PSEUDONANA(4,1)|THALASSIOSIRA WEISSFLOGII(4,1)|TRANSFORMATIONAL(4,1)|WATER REVERSIBLE CONVERSION(4,1)|WILBUR ANDERSON(4,1)|CELL LINE(3,9)|PLANT CONTROL(3,5)|BROAD BEAN(3,3)|BULB(3,3)|CO2(3,3)|GLYCINE MAX(3,3)|LBA(3,3)|P NITROPHENYL ACETATE(3,3)|PLANT GENOME(3,3)|TERM PARTIAL(3,3)|TALEN(3,2)|ACCESSION NUMBER GLYMA 19G(3,1)|ACTIVE PLANT OPERATION(3,1)|APOPTOSIS(3,1)|AQUEOUS ENVIRONMENT(3,1)|ARCHAEA(3,1)|BASE EDITOR(3,1)|BASE SUBSTITUTION(3,1)|BETA GLUCURONIDASE(3,1)|BICARBONATE LONG TERM SEQUESTRATION(3,1)|BIODIVERSITY(3,1)|BOTANICALLY DEFINED ROOT TISSUE(3,1)|BROMOCRESOL PURPLE(3,1)|CARBONATE CONSTRUCTION(3,1)|CARBONIC ANHYDRASE FUNCTION(3,1)||(CN120548358)|TRANSPORTABLE CARBONIC ANHYDRASE PROTEIN(100,20)|TRANSGENIC PLANT(100,13)|CARBON SEQUESTRATION(100,11)|HYDRASE(100,2)|CARBONIC ANHYDRASE PROTEIN(79,54)|CARBONIC ANHYDRASE(63,179)|PEPTIDE SEQUENCE(43,34)|ENHANCING SEQUESTRATION(42,1)|POLYPEPTIDE SEQUENCE(40,17)|DIRECTING TRANSPORT(36,4)|TRANSLOCATABLE CARBONIC ANHYDRASE PROTEIN(36,4)|EXPENSIVE PROFESSIONAL WASTE DISPOSAL(33,1)|VACUOLE SORTILIN(33,1)|SIGNAL PEPTIDE SEQUENCE(32,32)|EXPRESS ENZYME(32,1)|EXTRACELLULAR ENVIRONMENT(31,62)|PLANT CARBON SEQUESTRATION CAPACITY(29,4)|CARBONIC ANHYDRASE SEQUENCE(28,9)|MODIFIED PLANT EXPRESS(28,1)|CARBONIC ANHYDRASE DIRECTING TRANSPORT(27,2)|HERITABLE GENETIC MATERIAL(25,39)|PLANT ROOT EXTRACELLULAR ENVIRONMENT(25,7)|ALPHA CARBONIC ANHYDRASE(24,1)|POLYNUCLEOTIDE SEQUENCE(22,28)|PROGENY(22,10)|CARBON SEQUESTRATION CAPACITY(22,4)|AGROBACTERIUM SP(22,2)|ENZYME SEQUENCE(22,1)|PLANT PROTOPLAST(20,2)|PROTEIN SECRETORY PATHWAY(19,4)|CARROT PLANT(19,3)|PROCESSING PLANT PRODUCTION(19,3)|GERMPLASM(19,1)|EMBRYO(18,8)|POLYPEPTIDE ENCODING DNA(18,3)|ROOT CELL(17,55)|MODULAR SANDY COMPOST(17,4)|GROUND(16,55)|PLANT ROOT(16,44)|LEVINGTON ADVANCED F2S SEED(16,3)|PLANT ORGAN(15,7)|HAZARDOUS WASTE(15,1)|PLANT CELL(14,27)|SEQUESTRATION(14,10)|BIOREMEDIATION(14,4)|SEAWEED CARBONIC ANHYDRASE(14,4)|PLANT MODIFICATION(14,3)|IOTA SUBTYPE CARBONIC ANHYDRASE(14,2)|WASTE DISPOSAL(14,1)|SEED(13,11)|SORGHUM(13,7)|POLLEN GRAIN(13,6)|SECRET ABLE TRANSPORTABLE CARBONIC ANHYDRASE(13,5)|CARBONIC ANHYDRASE ACTIVITY PROTEIN(12,7)|PLANT CELL TRANSFORMATION(12,4)|ENDOGENOUS BASELINE EXPRESSION(12,3)|MIRACLE GRO(11,4)|TRANSMEMBRANE HELIX(11,4)|MELCOURT TOPSOIL(11,3)|MICROPARTICLE(11,3)|PSBP TRANSMEMBRANE DOMAIN(11,2)|VACUOLAR SORTING PROTEIN(11,2)|GLYCOSYL PHOSPHATIDYL INOSITOL(11,1)|HAKKERA DIATOM CARBONIC ANHYDRASE(11,1)|WAKAME KELP SEAWEED(11,1)|TRANSMEMBRANE SEQUENCE(10,7)|AGROBACTERIUM LB(10,5)|CARBONIC ANHYDRASE ENZYMATIC ACTIVITY(10,5)|SOYBEAN PLANT ENGINEER(10,5)|CELL CULTURE(10,3)|ESCHERICHIA(10,3)|EUCALYPTUS(10,3)|FRUIT(10,3)|GRASSLAND(10,3)|SWEET POTATO(10,3)|MATURE PLANT COMPOST(10,2)|ARABIDOPSIS PKY PROMOTER(10,1)|HIGHLIGHT CYTOPLASMIC GFP EXPRESSION(10,1)|POLYNUCLEOTIDE CARBONIC ANHYDRASE(10,1)|PLANT TISSUE(9,12)|SECRETED PROTEIN(9,4)|TRANSMEMBRANE DOMAIN SEQUENCE(9,4)|ALFALFA(9,3)|CLOVER(9,3)|MELCOURT GRIT(9,3)|MILLET(9,3)|SPECTROPHOTOMETRIC MICROPLATE READER(9,3)|SPRUCE(9,3)|CARBONIC ANHYDRASE SUBTYPE(9,2)|EXPERIMENTALLY CHARACTERIZED CARROT(9,2)|EXTRACELLULAR CARBONIC ANHYDRASE(9,2)|SUGAR BEET(9,2)|VETCH(9,2)|GUS STAINED ARABIDOPSIS THALIANA(9,1)|RICE PLANT(9,1)|GENETIC MATERIAL(8,40)|HYDROPONIC MEDIA(8,5)|EXPRESSION DOMAIN(8,4)|EXPRESSION REPRESENTATION(8,4)|ASPEN(8,3)|BARLEY(8,3)|CALLUS CULTURE(8,3)|CANOLA(8,3)|CRESS(8,3)|FLORAL DIP(8,3)|GENE EXPRESSION REGULATORY ELEMENT(8,3)|TOMATO(8,3)|PROCESSED PRODUCT(8,2)|CARBONIC ANHYDRASE CLASS(8,1)|ENDOGENOUS CARBONIC ANHYDRASE EXPRESSION(8,1)|ENGINEERED ARABIDOPSIS PLANT(8,1)|GAMMA CARBONIC ANHYDRASE(8,1)|GLYCOSYL PHOSPHATIDYLINOSITOL EXPRESSION(8,1)|MICROALGAE PSEUDOHAITANENSIS(8,1)|PEER UNTRANSFORMED ROOT(8,1)|ROOT SPECIFIC EXPRESSION(8,1)|SECRETED SOYBEAN CARBONIC ANHYDRASE(8,1)|CA PROTEIN(7,5)|HYDROPONIC SOLUTION(7,5)|COTTON(7,3)|GUS EXPRESSION(7,3)|NUCLEIC ACID SEQUENCE DETECTION(7,3)|PEA PLANT(7,3)|PINE(7,3)|TEFF(7,3)|WHEAT(7,3)|ZETA(7,3)|CARBONIC ANHYDRASE ASSAY(7,2)|CARBONIC ANHYDRASE TRANSPORTATION(7,2)|DRIVING OVER EXPRESSION(7,2)|HUMAN ACTIVITY(7,2)|SECRETED TRANSPORTED CARBONIC ANHYDRASE(7,2)|SOIL SAMPLING PROBE(7,2)|AGROBACTERIUM TUMEFASCIEN(7,1)|CALCIFIED PRIMORDIAL MESENCHYMAL CELL(7,1)|CARBONIC ANHYDRASE PROTEIN EXPRESSION(7,1)|CARROT EXPANSIN(7,1)|CONTICRIBRA WEISSFLOGII(7,1)|FUSION CARBONIC ANHYDRASE PROTEIN(7,1)|GASEOUS CO2 INTERCONVERSION(7,1)|MARINE ALGA CARBONIC ANHYDRASE(7,1)|OFFER INTERESTING OPPORTUNITY(7,1)|ORGANISM SKELETAL TISSUE(7,1)|SOYBEAN EXPANSIN GENE PROMOTER(7,1)|WEIHAIA CARBONIC ANHYDRASE(7,1)|CRISPR(6,8)|UNEQUAL VARIANCE(6,8)|FRAGMENT FUNCTION(6,4)|CORN(6,3)|ENGINEERED PLANT ROOT(6,3)|GENETICALLY MODIFIED PLANT(6,3)|HYDROPONIC BOX(6,3)|RUBBER TREE(6,3)|RYE(6,3)|ARABIDOPSIS ROOT(6,2)|COLORIMETRIC ASSAY(6,2)|GENE REPORTER FUSION(6,2)|HYDROPONIC TANK(6,2)|METLER PH PROBE(6,2)|MWCO PROTEIN CONCENTRATION COLUMN(6,2)|ROOT HOMOGENIZATION(6,2)|STABLE ENGINEERED STRAIN(6,2)|UNTRANSFORMED PLANT(6,2)|ABOVEGROUND BIOMASS(6,1)|BACTERIAL SELECTABLE MARKER(6,1)|BIOLOGICAL(6,1)|CARBONIC ANHYDRASE POLYPEPTIDE(6,1)|DONOR REPAIR TEMPLATE(6,1)|ENGINEERED CARBONIC ANHYDRASE(6,1)|EUKARYOTIC CARBONIC ANHYDRASE(6,1)|EXOGENOUS POLYNUCLEOTIDE(6,1)|GENETICALLY ENGINEERED ARABIDOPSIS(6,1)|GUS HISTOCHEMICAL(6,1)|INLAID CARBONIC ANHYDRASE(6,1)|INTRACELLULAR CARBONIC ANHYDRASE(6,1)|NONCONVENTIONAL SECRETORY PATHWAY(6,1)|PROTEIN NONROUTINE TRANSPORT(6,1)|SEAWEED WEGENER(6,1)|SOYBEAN PROTOPLAST CONFOCAL IMAGE(6,1)|TRANSFORMED PLANT REGENERATION(6,1)|WESTLAND JOHNINNE(6,1)|ELECTROPORATION(5,6)|GENETICALLY ENGINEERED PLANT(5,6)|GLYCOSYLPHOSPHATIDYLINOSITOL(5,6)|NONINTEGRATED CONTROL PLANT(5,5)|SEEDLING(5,5)|BICARBONATE ION(5,3)|BIOMASS PRODUCTION(5,3)|EXTRACTION BUFFER(5,3)|MEASURABLE DECREASE(5,3)|OIL PALM(5,3)|POSITIVE COLONY(5,3)|SOIL INORGANIC CARBON CONTENT(5,3)|UNIVERSAL SUSTAINED RELEASE(5,3)|BETA SUBTYPE(5,2)|CARBONIC ANHYDRASE ENDOGENOUS LEVEL(5,2)|CONCENTRATED HYDROPONIC MEDIUM SAMPLE(5,2)|ENDOGENOUS CARBONIC ANHYDRASE LEVEL(5,2)|GROWTH PHENOTYPE(5,2)|ME AGAR(5,2)|PHENOTYPIC DIFFERENCE(5,2)|PSPB SIGNAL PEPTIDE(5,2)|RECOMBINATION SITE(5,2)|RI PLASMID(5,2)|SOIL SLURRY(5,2)|SYNTHETIC PROMOTER(5,2)|ACTIVATED CARBONIC ANHYDRASE PROTEIN(5,1)|AEROPONIC GROWTH(5,1)|AGROBACTERIUM STRAIN(5,1)|AGROBACTERIUM TUMEFACIENS MEDIATED TRANSFORMATION(5,1)|CARBONIC ANHYDRASE COPY(5,1)|CARBONIC ANHYDRASE DRIVING EXPRESSION(5,1)|CARBONIC ANHYDRASE EXPRESSION PROTEIN(5,1)|CARBONIC ANHYDRASE MRNA(5,1)|CARBONIC ANHYDRASE VARIANT(5,1)|ENCODED CARBONIC ANHYDRASE(5,1)|FORMAL DIVERSITY(5,1)|GUS STAINING BUFFER(5,1)|INDUCIBLE PROMOTER(5,1)|INTEGRATED PLANT EXHIBITED BASELINE(5,1)|LYSOSOMAL SECRETION(5,1)|MONOMERIC SUBTYPE(5,1)|MULTIBASE SUBSTITUTION(5,1)|NATIVE CARBONIC ANHYDRASE SEQUENCE(5,1)|NATURALLY CATION ENRICHED SOIL(5,1)|NONPLANT ORGANISM(5,1)|NONSECRETORY PATHWAY(5,1)|POLYSACCHARIDE ANCHOR(5,1)|SEA URCHIN LARVA(5,1)|SECRET ABLE CARBONIC ANHYDRASE(5,1)|SEQUESTRATION MAGNITUDE(5,1)|SEXUAL BREEDING(5,1)|SOIL FLUX EXPERIMENT(5,1)|TARGETING NUCLEASE(5,1)|TRANSFECTED PROTOPLAST(5,1)|TRANSGENIC MANIPULATION(5,1)|TRANSGENIC SOYBEAN PLANT ROOT(5,1)|WEISSELLA VEYI(5,1)|CELL LINE(4,10)|STANDARD ERROR BAR(4,9)|PLANT TRANSFORMATION VECTOR(4,7)|ABSORBANCE(4,4)|BIOMOLECULE(4,4)|SPECTINOMYCIN(4,4)|SUPERNATANT(4,4)|ACETONITRILE(4,3)|BIOFUEL(4,3)|CULTIVAR(4,3)|DAUCUS CAROTA(4,3)|ENHANCER(4,3)|GENETIC ENGINEERING(4,3)|GLYCOPROTEIN(4,3)|PERLITE(4,3)|PISUM SATIVUM(4,3)|TERMINATOR(4,3)|AGROBACTERIUM RHIZOGENE(4,2)|BASELINE COMPARISON(4,2)|DIRECTING SECRETION TRANSPORT(4,2)|EXPERIMENTALLY CHARACTERIZED SIGNAL PEPTIDE(4,2)|RECORDING WINDOW(4,2)|TRISHCL SOLUTION(4,2)|ANCESTOR CELL(4,1)|AVERAGE CARBONIC ANHYDRASE(4,1)|BRUAD BEAN(4,1)|CA NUCLEASE(4,1)|CARBONIC ANHYDRASE ENZYME ACTIVITY(4,1)|CARBONIC ANHYDRASE MODIFICATION(4,1)|CARBONIC ANHYDRASE PROTEIN PRODUCTION(4,1)|CARBONIC ANHYDRASE SECRETION TRANSPORT(4,1)|CASTOR BEAN CATALASE(4,1)|CELLULAR EXPORT(4,1)|CLASSICAL GENETIC MODIFICATION(4,1)|CLONAL PROPAGATION(4,1)|COVERING BARE SOIL(4,1)|CRUSHED STONE GROUND TREATMENT(4,1)|DIVERSE CONTEXT(4,1)|DRIED BIOMASS(4,1)|ENDOGENOUS EXPRESSION(4,1)|ENZYME DISTRIBUTION(4,1)|EXOGENOUS SOIL TREATMENT(4,1)|EXOSOME RELEASE(4,1)|EXTRACELLULAR EXPRESSION(4,1)|EXTRACELLULAR MEMBRANE(4,1)|GAMMA SUBTYPE(4,1)|GENE EDITING PROTEIN(4,1)|GENE PSBP(4,1)|GENETICALLY ENGINEERED SOYBEAN PLANT(4,1)|GENETICALLY ENGINEERED SOYBEAN ROOT(4,1)|GLYCINE MAX(4,1)|GUIDED EDITING(4,1)|GUS STAINED ROOT REGION(4,1)|HAIRY ROOT TISSUE(4,1)|HAIRY ROOT TRANSFORMATION(4,1)|HARVEST ABLE SEED(4,1)|HCO CONVERSION(4,1)|HIGHLIGHT FLUORESCENT PROTEIN(4,1)|HOMOGENIZED ROOT SAMPLE(4,1)|HORTICULTURAL PLANT(4,1)|HOST GENOME(4,1)|HYDROPONIC GROWTH ENVIRONMENT(4,1)|ISOLATED PROTEIN SAMPLE(4,1)|JOHN LNES(4,1)|LEADER PEPTIDE(4,1)|LIVING TREE LIFE FORM(4,1)|MACROMOLECULE TRANSPORT(4,1)|MEMBRANE ANCHORING(4,1)|MINIATURE PLANT CHAMBER(4,1)|MODIFIED CARBONIC ANHYDRASE IMMOBILIZED(4,1)|MOSAIC VIRUS PROMOTER(4,1)|NONENGINEERED PLANT(4,1)|NONINTEGRATED PLANT(4,1)|NONLIMITING SENSE(4,1)|NONNATURAL PLANT(4,1)|ONEVIEW CAMERA(4,1)|PARIS AGREEMENT(4,1)|PLANT NODULE(4,1)|POLYNUCLEOTIDE ISOLATION(4,1)|POSITIVE TRANSFORMED ROOT TISSUE(4,1)|POSITIVELY CHARGED CATION(4,1)|PROMOTER GUS FUSION(4,1)|PROTEIN CONSTRUCT(4,1)|PROTEIN SECRETION TRANSPORT(4,1)|PROTOZOA SPECIES(4,1)|PSBP SIGNAL PEPTIDE(4,1)|RNA COATED PARTICLE BOMBARDMENT(4,1)|ROOT HAIR CYTOPLASMIC MEMBRANE(4,1)|ROOT PROMOTER(4,1)|SEMIAQUATIC PLANT(4,1)|SILICATE ROCK(4,1)|SLAKED LIME CA(4,1)|SOYBEAN PLASMA MEMBRANE(4,1)|SOYBEAN ROOT HAIR(4,1)|SOYBEAN TRANSFORMATION(4,1)|SUBSTITUTION GENOME EDITING(4,1)|TARGET PLANT(4,1)|TARGETING PEPTIDE(4,1)|TRANSGENIC PLANT ROOT(4,1)|TRANSGENIC ROOT SAMPLE(4,1)|TRANSIT PEPTIDE(4,1)|TRANSLATION TEMPLATE(4,1)|UNDERGROUND ROOT(4,1)|UNMODIFIED PLANT(4,1)|VIRAL TRANSFECTION(4,1)|WILD PEA(4,1)|PLANT ROOT CELL(3,10)|HERBICIDE RESISTANCE(3,6)|GRNA(3,5)|PERCENT HOMOLOGY(3,5)|SEQUENCE IDENTITY(3,5)|PROTON(3,4)|INTERNAL ENVIRONMENT(3,3)|BIOLISTIC(3,2)|BROMOTHYMOL BLUE(3,2)|BURKHOLDERIA(3,2)|CARBONIC ANHYDRASES(3,2)|CULTIVATED LAND(3,2)|FLOWERING(3,2)|FORESTRY(3,2)|HYDRATION(3,2)|KANAMYCIN(3,2)|MEGANUCLEASE(3,2)|MICROINJECTION(3,2)|PHOTOGRAPH(3,2)|PLANT SELECTION MARKER(3,2)|RAINWATER(3,2)|REPORTER GENE(3,2)|REVERSE REACTION(3,2)|SAMPLE FILTRATION(3,2)|SAMPLE TOTAL PROTEIN(3,2)|SOIL RESPIRATION(3,2)|SOIL WEIGHT(3,2)|TALE NUCLEASE(3,2)|TUBER(3,2)|VERSION MODIFICATION(3,2)|ACTIVE PROMOTER(3,1)|AGROECOLOGICAL(3,1)|ANCHOR MOLECULE(3,1)|ATMOSPHERIC CARBON SEQUESTRATION(3,1)|BRASSICA OLERACEA(3,1)|CARBONIC ANHYDRASE CODING SEQUENCE(3,1)|CARBONIC ANHYDRASE INCREASED EXPRESSION(3,1)|CARBONIC ANHYDRASE PROTEIN SEQUENCE(3,1)|CARBONIC ANHYDRASE SOLUTION(3,1)|CATALYTIC REMOVAL(3,1)|COMPOUND ABSORPTION(3,1)|CONSTRUCT FEATURE(3,1)|CONVERSION ENHANCEMENT(3,1)|CROP PLANT SPECIES(3,1)|CULTIVATION REST PERIOD(3,1)|ENZYMATIC ACTIVITY ASSAY(3,1)|ENZYME LABELED INSTRUMENT(3,1)|EXCESS HYDROPONIC MEDIUM(3,1)|EXPRESSION ENHANCEMENT(3,1)|FERTILIZER TREATMENT(3,1)|GENETICALLY ENHANCED PLANT(3,1)|GROWTH CYCLE(3,1)|HYDROPONIC CONDITION(3,1)|ICE COLD PESTLE(3,1)|IMMEDIATE ENVIRONMENT(3,1)|INORGANIC CARBON SEQUESTRATION(3,1)|INORGANIC ION(3,1)|JOINT EFFORT(3,1)|LIFE DOMAIN(3,1)|LOCALIZATION SEQUENCE(3,1)|MEMBRANE BOUND PROTEIN(3,1)|MERISTEMATIC REGION(3,1)|MOISTURE ABSORPTION(3,1)|NATIVE REGULATORY SEQUENCE(3,1)|NATURAL ENVIRONMENT(3,1)|NATURALLY OCCURRING PROMOTER(3,1)|NET CARBON SEQUESTRATION(3,1)|OBSERVABLE NEGATIVE(3,1)|PH CHANGEOVER RATE(3,1)|PLANT EXPRESSION VECTOR(3,1)|PLANT ROOT TISSUE(3,1)|POSTTRANSLATIONAL(3,1)|PRODUCED CARBONIC ANHYDRASE PROTEIN(3,1)|ROOT ENVIRONMENT(3,1)|ROOT ENZYME ACTIVITY(3,1)|ROOT TIP EPIDERMIS(3,1)|ROW CROP PLANT(3,1)|SEQUESTRATION SOLUTION(3,1)|SOIL DRYING(3,1)|SOIL NUTRIENT CONTENT(3,1)|SOIL PH TESTER(3,1)|SOYBEAN ROOT CELL(3,1)|STABLE TRANSFORMATION(3,1)|SUBCELLULAR LOCALIZATION(3,1)|TEMPLATE SEQUENCE(3,1)|TERRESTRIAL ECOSYSTEM(3,1)|THALASSIOSIRA PSEUDONANA(3,1)|THALASSIOSIRA WEISSFLOGII(3,1)|WATER REVERSIBLE CONVERSION(3,1)|WILD TYPE PLANT(2,9)|FLUORESCENT PROTEIN CODING SEQUENCE(2,4)|LBA(2,3)|P NITROPHENYLACETATE(2,3)|PLANT GENOME(2,3)|WATER CULTURE MEDIUM(2,3)|CEREAL(2,2)|DIMER(2,2)|NONHOMOLOGOUS END JOINING REPAIR(2,2)|RETENTION(2,2)|ACCELERATE LONG TERM SEQUESTRATION(2,1)|ACCESSION NUMBER GLYMA 19G(2,1)|APOPTOSIS(2,1)|AQUEOUS CULTURE SOLUTION(2,1)|AQUEOUS ENVIRONMENT(2,1)|ARCHAEA(2,1)|ASEXUAL PROPAGATION(2,1)|ASEXUAL REPRODUCTION(2,1)|ASPERGILLUS(2,1)|AVERAGE INORGANIC CARBON CONTENT(2,1)|BASE EDITOR(2,1)|BETA GLUCURONIDASE(2,1)|BIOCHEMISTRY(2,1)|BIODIVERSITY(2,1)|BIOINFORMATICS(2,1)|BLEBBING(2,1)|BROMOCRESOL PURPLE(2,1)|CABBAGE(2,1)|CASSAVA VEIN MOSAIC VIRUS(2,1)|CELL EXTERIOR(2,1)|CELL PERIPHERY(2,1)|CELL TARGET PROTEIN(2,1)|CENTRIFUGATION(2,1)|CONFOCAL MICROSCOPE(2,1)|CONTROLLED BREEDING(2,1)|COVER CROP PLANT(2,1)|COWPEA(2,1)|CYTOPLASMIC LOCALIZATION CONTROL(2,1)|DESALINIZATION(2,1)||(IN202517071665)|TRANSPORTABLE CARBONIC ANHYDRASE PROTEIN(100,24)|TRANSGENIC PLANT(100,12)|CARBON SEQUESTRATION(100,8)|HYDRASE(100,3)|CARBONIC ANHYDRASE PROTEIN(80,54)|CARBONIC ANHYDRASE(63,187)|CARBONIC ANHYDRASE DIRECTING TRANSPORT(48,4)|ANTHROPOGENIC CO2 RELEASE ISSUE(46,1)|TRANSMEMBRANE HELIX(45,4)|ATMOSPHERIC CO2 ENHANCING SEQUESTRATION(42,1)|TRANSMEMBRANE DOMAIN(40,21)|EXPRESS CARBONIC ANHYDRASE(40,1)|ANTHROPOGENIC CO2 RELEASE(39,1)|PEPTIDE SEQUENCE(38,33)|ENHANCING SEQUESTRATION(38,1)|POLYPEPTIDE SEQUENCE(33,17)|EXPENSIVE SPECIALIST WASTE DISPOSAL(33,1)|VACUOLAR SORTING PROTEIN(31,3)|EXTRACELLULAR ENVIRONMENT(30,60)|DIRECTING TRANSPORT(30,6)|SIGNAL PEPTIDE SEQUENCE(29,31)|GLYCOSYLPHOSPHATIDYLINOSITOL(28,6)|CARBONIC ANHYDRASE SEQUENCE(27,9)|CONTICRIBRA WEISSFLOGII CARBONIC ANHYDRASE(26,6)|PLANT PROTOPLAST(26,5)|HERITABLE GENETIC MATERIAL(24,37)|ELEVATED ATMOSPHERIC CO2(24,1)|BIOREMEDIATION(23,4)|MEMBRANE ANCHORING(23,2)|PRAIRIE GRASS(22,3)|PLANT MODIFICATION(21,4)|EXTENSIN PROTEIN(21,3)|CARBONIC ANHYDRASE TRANSPORT(20,6)|BIOMOLECULE(20,5)|AGROBACTERIUM SP(20,3)|BREEDING PROGRAM(20,1)|ROOT EPIDERMIS(19,2)|POLYNUCLEOTIDE SEQUENCE(18,23)|SECRETION(18,5)|CARROT PLANT(18,3)|PROCESSING PLANT PRODUCTION(18,3)|GERMPLASM(18,1)|INCORPORATION(18,1)|PLANT CARBON SEQUESTRATION ABILITY(18,1)|ROOT TISSUE(17,4)|PROTEIN SECRETION PATHWAY(17,3)|BYPRODUCT(17,1)|ROOT CELL(16,58)|PROGENY(16,10)|EMBRYO(16,8)|CROP(16,4)|LEVINGTON ADVANCE F2S SEED(16,4)|PROMOTOR(16,4)|POLYPEPTIDE CODING DNA(16,3)|PLASMA MEMBRANE(15,22)|AGROBACTERIUM TUMEFASCIEN(15,5)|GROUND(14,51)|PLANT ROOT(14,41)|PLANT ORGAN(14,7)|CO2 SEQUESTRATION(14,4)|HAZARDOUS WASTE(14,1)|ATMOSPHERIC CO2(13,9)|CODING SEQUENCE(13,9)|ANCHOR(13,6)|HERITABLE GENETIC MATERIAL ALTERING(13,6)|WASTE DISPOSAL(13,1)|PLANT CELL(12,28)|SEED(12,12)|CARBONIC ANHYDRASE ACTIVITY PROTEIN(12,7)|AGROBACTERIUM LB(11,6)|POLLEN GRAIN(11,6)|SECRET ABLE TRANSPORTABLE CARBONIC ANHYDRASE(11,5)|MICROPARTICLE(11,4)|ENDOGENOUS BASELINE EXPRESSION(11,3)|LEVINGTON M3 COMPOST(11,2)|SOILS(11,2)|DIATOM CONTICRIBRA WEISSFLOGII(11,1)|TRANSMEMBRANE SEQUENCE(10,7)|TREE(10,7)|SEQUESTER CARBON(10,4)|EUCALYPTUS(10,3)|FRUIT(10,3)|MELCOURT SHARP SAND(10,3)|MELCOURT TOPSOIL(10,3)|PLANT TISSUE(9,12)|CARBONIC ANHYDRASE ENZYMATIC ACTIVITY(9,6)|CARBONIC ANHYDRASE ENDOGENOUS LEVEL(9,4)|CROP PLANT(9,4)|EXPERIMENTALLY CHARACTERIZED SIGNAL PEPTIDE(9,4)|REPRESENTATIVE WORDING(9,4)|SAND COMPOST(9,4)|SECRETED PROTEIN(9,4)|ALFALFA(9,3)|CELL CULTURE(9,3)|CLOVER(9,3)|MILLET(9,3)|POPLAR(9,3)|SPRUCE(9,3)|SWEET POTATO(9,3)|GASEOUS CO2 INTERCONVERSION(9,2)|FUNGUS ASPERGILLUS FICUUM(9,1)|GUS HISTOCHEMICAL STAINING(9,1)|HIGHLIGHT CYTOPLASMIC GFP EXPRESSION(9,1)|LONG TERM CO2 SEQUESTRATION(9,1)|RICE PLANT(9,1)|BICARBONATE ION(8,5)|HYDROPONIC BOX(8,5)|SOYBEAN PLANT ENGINEER(8,5)|CARBONIC ANHYDRASE INCREASED LEVEL(8,2)|CARBONIC ANHYDRASE SUBTYPE(8,2)|ENDOGENOUS CARBONIC ANHYDRASE(8,2)|PROCESSED PRODUCT(8,2)|ROOT SPECIFIC EXPRESSION(8,1)|SECRETED SOYBEAN CARBONIC ANHYDRASE(8,1)|GENETIC MATERIAL(7,38)|CRISPR(7,10)|CO2 CONVERSION(7,6)|HYDROPONIC SOLUTION(7,6)|ROOT CELL PROMOTER(7,6)|PERCENTAGE IDENTITY(7,4)|ATMOSPHERIC CO2 SEQUESTRATION(7,3)|BARLEY(7,3)|CALLUS CULTURE(7,3)|CANOLA(7,3)|CORN(7,3)|COTTON(7,3)|CRESS(7,3)|EXTRACELLULAR ENVIRONMENT CARBONIC ANHYDRASE(7,3)|GENE EXPRESSION REGULATORY ELEMENT(7,3)|GUS EXPRESSION(7,3)|NUCLEIC ACID SEQUENCE DETECTION(7,3)|PEA PLANT(7,3)|PINE(7,3)|SUGAR BEET(7,3)|TEFF(7,3)|TOMATO(7,3)|VETCH(7,3)|WHEAT(7,3)|DRIVING OVER EXPRESSION(7,2)|ICE CHILLED CO2(7,2)|MIRACLE GRO(7,2)|MODIFIED CARBONIC ANHYDRASE(7,2)|PLANT SELECTABLE MARKER(7,2)|SECRET ABLE CARBONIC ANHYDRASE(7,2)|SECRETED TRANSPORTED CARBONIC ANHYDRASE(7,2)|AGROBACTERIUM TUMEFACIENS MEDIATED TRANSFORMATION(7,1)|CARBONIC ANHYDRASE ENDOGENOUS EXPRESSION(7,1)|ENGINEERED ARABIDOPSIS THALIANA PLANT(7,1)|EXTRACELLULAR ROOT CARBONIC ANHYDRASE(7,1)|MEDIATED CO2 SEQUESTRATION(7,1)|MICROALGAE THALASSIOSIRA PSEUDONANA(7,1)|STAINED ARABIDOPSIS THALIANA ROOT(7,1)|TAGGED CARBONIC ANHYDRASE PROTEIN(7,1)|UNEQUAL VARIANCE(6,8)|AZYGOUS CONTROL PLANT(6,7)|CA PROTEIN(6,5)|DNA POLYNUCLEOTIDE SEQUENCE(6,4)|FRAGMENT FUNCTION(6,4)|ROOT EXTRACELLULAR ENVIRONMENT(6,4)|CONTAINED ENGINEERED PLANT(6,3)|EXPRESSION DOMAIN(6,3)|GLYCINE MAX(6,3)|GROUND BIOMASS(6,3)|RYE(6,3)|ARABIDOPSIS ROOT(6,2)|AZYGOUS PLANT(6,2)|COLORIMETRIC ASSAY(6,2)|CONCENTRATED HYDROPONIC MEDIA SAMPLE(6,2)|EXTRACELLULAR MEMBRANE(6,2)|EXTRACELLULAR ROOT ENVIRONMENT(6,2)|GENE REPORTER FUSION(6,2)|MULTICLONING SITE(6,2)|PERLITE SOIL(6,2)|SEQUESTERING CO2(6,2)|TARGETING PEPTIDE(6,2)|TRANSGENIC MANIPULATION(6,2)|TRANSPORT CARBONIC ANHYDRASE(6,2)|UNTRANSFORMED PLANT(6,2)|BACTERIAL SELECTABLE MARKER(6,1)|CARBONIC ANHYDRASE ESTERASE(6,1)|CARBONIC ANHYDRASE POLYPEPTIDE(6,1)|CARROT EXTENSIN(6,1)|CLEAR CYTOSOLIC LOCALIZATION(6,1)|CO2 SOIL FLUX EXPERIMENT(6,1)|DONOR REPAIR TEMPLATE(6,1)|ENGINEERED CARBONIC ANHYDRASE(6,1)|ENGINEERED SOYBEAN HAIRY ROOT(6,1)|EUKARYOTIC CARBONIC ANHYDRASE(6,1)|EXOGENOUS POLYNUCLEOTIDE(6,1)|EXTRACELLULAR CARBONIC ANHYDRASE(6,1)|EXTRACELLULAR CO2 HYDRATION(6,1)|FUSION CARBONIC ANHYDRASE PROTEIN(6,1)|GUS STAINED ROOT(6,1)|HARNESSING CARBONIC ANHYDRASE(6,1)|INTRACELLULAR CARBONIC ANHYDRASE(6,1)|MATURE PLANT COMPOST(6,1)|ORGANISM SKELETAL TISSUE(6,1)|POLYNUCLEOTIDE CARBONIC ANHYDRASE(6,1)|POSITIVELY TRANSFORMED ROOT TISSUE(6,1)|PROTEIN NONCONVENTIONAL TRANSPORT(6,1)|RADIO TRACER ASSAY(6,1)|RNACOATED PARTICLE BOMBARDMENT(6,1)|SOYBEAN EXPANSIN GENE PROMOTER(6,1)|SOYBEAN PROTOPLAST CONFOCAL IMAGE(6,1)|SOYBEAN PROTOPLAST PLASMA MEMBRANE(6,1)|TRANSFECTED PROTOPLAST(6,1)|TRANSFORMED PLANT REGENERATION(6,1)|VISUAL REPORTER EXPRESSION(6,1)|ELECTROPORATION(5,6)|GENETICALLY ENGINEERED PLANT(5,6)|TAILED STUDENT T TEST(5,6)|CELL WALL(5,5)|HOMOLOGY(5,5)|N TERMINUS(5,5)|BIOMASS PRODUCTION(5,3)|DIRECTING SECRETION TRANSPORT(5,3)|EXTRACTION BUFFER(5,3)|MEASURABLE DECREASE(5,3)|ORDINARY SKILL PERSON(5,3)|PISUM SATIVUM(5,3)|POSITIVE COLONY(5,3)|SHOW CARBONIC ANHYDRASE(5,3)|SOIL INORGANIC CARBON CONTENT(5,3)|DIAMETER SOIL SAMPLER PROBE(5,2)|DRIED BIOMASS(5,2)|ENGINEERED PLANT ROOT(5,2)|ENHANCE CO2 SEQUESTRATION(5,2)|GROWTH PHENOTYPE(5,2)|ME AGAR(5,2)|MEMBRANE ANCHORING SEQUENCE(5,2)|RECOMBINATION SITE(5,2)|RI PLASMID(5,2)|SOIL SLURRY(5,2)|SYNTHETIC PROMOTER(5,2)|AEROPONIC GROWTH(5,1)|AGROBACTERIUM RHIZOGENE STRAIN(5,1)|AGROBACTERIUM STRAIN(5,1)|CARBONIC ANHYDRASE ASSAY(5,1)|CARBONIC ANHYDRASE DRIVING EXPRESSION(5,1)|CARBONIC ANHYDRASE MRNA(5,1)|CARBONIC ANHYDRASE VARIANT(5,1)|CHILLED PESTLE(5,1)|DIFFERING POLYNUCLEOTIDE PEPTIDE SEQUENCE(5,1)|ENCODED CARBONIC ANHYDRASE(5,1)|GENETICALLY ENGINEERED ARABIDOPSIS(5,1)|GRAM NEGATIVE BACTERIUM BURKHOLDERIA(5,1)|GUS STAINING BUFFER(5,1)|HANNATM SOIL PH TESTER(5,1)|HIGHLIGHT FLUORESCENT PROTEIN EXPRESSION(5,1)|HOMOGENIZED ROOT SAMPLE(5,1)|INDUCIBLE PROMOTER(5,1)|INTERESTING OPPORTUNITY(5,1)|LYSOSOMAL SECRETION(5,1)|METLER PH PROBE(5,1)|MICROALGAE SPECIES(5,1)|MONOMERIC SUBTYPE(5,1)|NATIVE CARBONIC ANHYDRASE SEQUENCE(5,1)|NONENGINEERED PLANT(5,1)|POLYSACCHARIDE ANCHOR(5,1)|SEA URCHIN LARVA(5,1)|SEQUESTRATION MAGNITUDE(5,1)|SIGNALING PEPTIDE(5,1)|SOYBEAN ROOT HAIR(5,1)|TALE NUCLEASE(5,1)|UNCONVENTIONAL SECRETORY PATHWAY(5,1)|WILDTYPE ROOT ENVIRONMENT(5,1)|WORD CARBONIC ANHYDRASE(5,1)|COVER CROP(4,7)|PLANT TRANSFORMATION VECTOR(4,7)|ABSORBANCE(4,4)|PROTON(4,4)|SPECTINOMYCIN(4,4)|SUPERNATANT(4,4)|GLYCOPROTEIN(4,3)|OIL PALM(4,3)|BASELINE COMPARISON(4,2)|CELL STRAINER(4,2)|CO2 TURN CATALYZED CONVERSION(4,2)|DISCERNIBLE DIFFERENCE(4,2)|HYDROPONIC MEDIUM SAMPLE(4,2)|MEMBRANE BOUND PROTEIN(4,2)|PLANT CELL GENOME(4,2)|SUPER FOLD(4,2)|WASHING(4,2)|CARBONIC ANHYDRASE DETECTION(4,1)|CARBONIC ANHYDRASE PROTEIN PRODUCTION(4,1)|CARBONIC ANHYDRASE SECRETION TRANSPORT(4,1)|CASTOR BEAN CATALASE(4,1)|CELLULAR EXPORT(4,1)|CLONAL PROPAGATION(4,1)|CO2 SEQUESTRATION FACILITATION(4,1)|EXCESS HYDROPONIC MEDIA(4,1)|EXOGENOUS SOIL TREATMENT(4,1)|EXTRACELLULAR EXPRESSION(4,1)|EXTRACORPOREAL CO2 REMOVAL(4,1)|FLORAL DIPPING(4,1)|GENETICALLY ENGINEERED SOYBEAN ROOT(4,1)|HAIRY ROOT TRANSFORMATION(4,1)|HCO3 ENHANCED CONVERSION(4,1)|HORTICULTURAL PLANT(4,1)|HYDROPONIC GROWTH ENVIRONMENT(4,1)|LEADER PEPTIDE(4,1)|MEAN CARBONIC ANHYDRASE(4,1)|MITIGATE SOIL EROSION(4,1)|MWCO PROTEIN(4,1)|NA2EDTA H2O(4,1)|ONEVIEW CAMERA(4,1)|PLANT NODULE(4,1)|PRIME EDITING(4,1)|PROMOTER GUS FUSION(4,1)|PROTEIN CONCENTRATION(4,1)|PROTEIN SECRETORY PATHWAY(4,1)|RELEASING ENZYME(4,1)|REPORTER GENE FUSION(4,1)|SEEDLING ROOT(4,1)|SEMIAQUATIC PLANT(4,1)|SOIL GROWN PLANT(4,1)|SORGHUM RICE(4,1)|SOYBEAN TRANSFORMATION(4,1)|TARGETED NUCLEASE(4,1)|TRANSGENIC ROOT SAMPLE(4,1)|TRANSGENIC SOYBEAN PLANT(4,1)|TRANSIT PEPTIDE(4,1)|VIRAL TRANSFECTION(4,1)|WEED PEST MANAGEMENT(4,1)|HERBICIDE RESISTANCE(3,6)|GRNA(3,5)|SEQUENCE IDENTITY(3,5)|ACETONITRILE(3,3)|BIOFUEL(3,3)|CULTIVAR(3,3)|DAUCUS CAROTA(3,3)|ENHANCER(3,3)|FALLOW PERIOD(3,3)|GENETIC ENGINEERING(3,3)|INTERNAL ENVIRONMENT(3,3)|SPECTROPHOTOMETER PLATE READER(3,3)|TERMINATOR(3,3)|ARABLE LAND(3,2)|ASEXUAL REPRODUCTION(3,2)|BROMOTHYMOL BLUE(3,2)|CASSAVA VEIN MOSAIC VIRUS(3,2)|CONVERSION ENHANCEMENT(3,2)|EQUILIBRIUM(3,2)|FLOWERING(3,2)|FORESTRY(3,2)|INCREASED ACCUMULATION(3,2)|INCREASED CARBONIC ANHYDRASE(3,2)|INORGANIC SOIL CARBON(3,2)|KANAMYCIN(3,2)|MICROINJECTION(3,2)|P NITROPHENYL HYDROLYSIS(3,2)|PLANT PRODUCTION(3,2)|REMAINING SOIL(3,2)|SAMPLE FILTRATION(3,2)|SOIL RESPIRATION(3,2)|TALEN(3,2)|TUBER(3,2)|ABSORPTION COMPOUND(3,1)|ACTIVE ENGINEERED PLANT(3,1)|AGROECOSYSTEM(3,1)|ANCESTOR CELL(3,1)|ANCHOR MOLECULE(3,1)|ANIMAL CONSUMPTION(3,1)|ANTHROPOGENIC GREENHOUSE GAS EMISSION(3,1)|BACKWARD REACTION(3,1)|BICARBONATE SALT(3,1)|BRASSICA OLERACEA(3,1)|CA NUCLEASE(3,1)|CALLUS TISSUE(3,1)|CARBONIC ANHYDRASE ADAPTATION(3,1)|CARBONIC ANHYDRASE CODING SEQUENCE(3,1)|CARBONIC ANHYDRASE ENZYME ACTIVITY(3,1)|CARBONIC ANHYDRASE INCREASED EXPRESSION(3,1)|CARBONIC ANHYDRASE SOLUTION(3,1)|CHOICE SPECIES(3,1)|CO2 DISSOLUTION(3,1)|CO2 ENHANCED CONVERSION(3,1)|CONFERRED GENE EXPRESSION(3,1)|CONTRIBUTOR(3,1)|CROP PLANT SPECIES(3,1)|CRUSHED ROCK SOIL TREATMENT(3,1)|CYTOPLASMIC LOCALIZED CONTROL(3,1)|DOUBLE STRANDED BREAK(3,1)|ENHANCED CO2 SEQUESTRATION(3,1)|ENTIRE GLYCOPHOSPHATIDYLINOSITOL(3,1)|ENZYME ACTIVITY ASSAY(3,1)|ENZYME DISTRIBUTION(3,1)|ENZYME SEQUENCE(3,1)|EX VIVO EX PLANT(3,1)|EXOSOME RELEASE(3,1)|EXPRESSION ENHANCEMENT(3,1)|FERTILIZER TREATMENT(3,1)|GASEOUS CARBON DIOXIDE INTERCONVERSION(3,1)|GENE EDITING PROTEIN(3,1)|GENETICALLY ENGINEERED SOYBEAN PLANT(3,1)|GENETICALLY ENHANCED PLANT(3,1)|GRAMNEGATIVE BACTERIA(3,1)|HARVEST ABLE SEED(3,1)|HOST GENOME(3,1)|HYDROPONIC CONDITION(3,1)|IMMEDIATE ENVIRONMENT(3,1)|INORGANIC CARBON SEQUESTRATION(3,1)|INORGANIC ION(3,1)|ISOLATED PROTEIN SAMPLE(3,1)|LIFE DOMAIN(3,1)|LOCALIZATION SEQUENCE(3,1)|MERISTEMATIC REGION(3,1)|MULTIMER FORMATION(3,1)|NATIVE REGULATORY SEQUENCE(3,1)|NATURALLY OCCURRING ENZYME(3,1)|NATURALLY OCCURRING PROMOTER(3,1)|NET CARBON SEQUESTRATION(3,1)|NUTRIENT CONTENT(3,1)|OBSERVABLE NEGATIVE(3,1)|PGMPIN2B PROMOTER CONTROL(3,1)|PLANT EXPRESSION VECTOR(3,1)|PLANT ROOT TISSUE(3,1)|POLYNUCLEOTIDE ISOLATION(3,1)|POLYPEPTIDE ISOLATION(3,1)|PRIMARY MESENCHYME CELL CALCIFICATION(3,1)|PROTEIN ASSAY(3,1)|PROTEIN CONSTRUCT(3,1)|PROTOCOL ADAPTED VERSION(3,1)|RECORDING WINDOW(3,1)|REDUCING GLOBAL CO2 EMISSION(3,1)|ROOT PROMOTER SEQUENCE(3,1)|ROOT SPECIFIC PROMOTER VARIANT(3,1)|ROOTSPECIFIC CELL(3,1)|SEA FLOOR(3,1)|SNAP LID MICROCENTRIFUGE TUBE(3,1)|SOIL CO2 SEQUESTRATION RATE(3,1)|SOYBEAN ROOT CELL(3,1)|STABLE TRANSFORMATION(3,1)|SUBCELLULAR LOCALIZATION(3,1)|SUPER RANDOM LOCATION(3,1)|TARGET PEPTIDE(3,1)|TARGET PLANT(3,1)|TEMPLATE SEQUENCE(3,1)|TERRESTRIAL ECOSYSTEM(3,1)|THALASSIOSIRA WEISSFLOGII(3,1)|TRISHCL SOLUTION(3,1)|UNMODIFIED PLANT(3,1)|UNQUALIFIED SENSE(3,1)|VEGETATIVE CYCLE(3,1)|WATER REVERSIBLE CONVERSION(3,1)|WILD TYPE PLANT(2,9)|DNA SEQUENCE(2,6)|CARBONIC ANHYDRASE EXPRESSION(2,4)|FIVE FOLD(2,3)|NONHOMOLOGOUS END JOINING REPAIR(2,2)|ACCESSION NUMBER GLYMA 19G(2,1)|ACCLIMATIZATION(2,1)|ADZUKI BEAN(2,1)|ANCHORAGE(2,1)|APOPTOSIS(2,1)|AQUEOUS ENVIRONMENT(2,1)|ARABLE FARMING(2,1)|ARCHAEA(2,1)|AVERAGE SKILL(2,1)|BASE EDITOR(2,1)|BASE SUBSTITUTION(2,1)|BETA GLUCURONIDASE(2,1)|BIOCHEMISTRY(2,1)|BIODIVERSITY(2,1)|BIOINFORMATICS(2,1)|BIOLISTIC(2,1)|BLEBBING(2,1)|BOTANY(2,1)|BROMOCRESOL PURPLE(2,1)|C4 PHOTOSYNTHESIS(2,1)|CARBONIC ANHYDRASE LEVEL(2,1)|CELL EXTRACELLULAR ENVIRONMENT(2,1)|CELL TARGET PROTEIN(2,1)|CEREAL(2,1)|CHAMBER COVER(2,1)|CHLOROPHYL(2,1)|COLOR CHANGE(2,1)|COMBINED EFFORT(2,1)|CONFOCAL MICROSCOPE(2,1)|CONTROL ARABIDOPSIS THALIANA PLANT(2,1)|CONTROLLED BREEDING(2,1)|COWPEA(2,1)||(AU2024206960)|PLANT(100,154)|GROUND(100,49)|GENETIC MATERIAL(100,39)|HERITABLE GENETIC MATERIAL(100,38)|TRANSPORTABLE CARBONIC ANHYDRASE PROTEIN(100,24)|POLYNUCLEOTIDE SEQUENCE(100,23)|TRANSGENIC PLANT(100,12)|CARBON SEQUESTRATION(100,8)|SEQUESTER CARBON(100,4)|HYDRASE(100,2)|CARBONIC ANHYDRASE PROTEIN(80,54)|CARBONIC ANHYDRASE(63,185)|CARBONIC ANHYDRASE DIRECTING TRANSPORT(48,4)|ANTHROPOGENIC CO2 RELEASE ISSUE(46,1)|TRANSMEMBRANE HELIX(45,4)|ATMOSPHERIC CO2 ENHANCING SEQUESTRATION(42,1)|TRANSMEMBRANE DOMAIN(40,21)|EXPRESS CARBONIC ANHYDRASE(40,1)|ANTHROPOGENIC CO2 RELEASE(39,1)|PEPTIDE SEQUENCE(38,33)|ENHANCING SEQUESTRATION(38,1)|POLYPEPTIDE SEQUENCE(33,17)|EXPENSIVE SPECIALIST WASTE DISPOSAL(33,1)|VACUOLAR SORTING PROTEIN(31,3)|EXTRACELLULAR ENVIRONMENT(30,60)|DIRECTING TRANSPORT(30,6)|SIGNAL PEPTIDE SEQUENCE(29,31)|GLYCOSYLPHOSPHATIDYLINOSITOL(28,6)|CARBONIC ANHYDRASE SEQUENCE(27,9)|CONTICRIBRA WEISSFLOGII CARBONIC ANHYDRASE(26,6)|PLANT PROTOPLAST(26,5)|ELEVATED ATMOSPHERIC CO2(24,1)|BIOREMEDIATION(23,4)|MEMBRANE ANCHORING(23,2)|PRAIRIE GRASS(22,3)|PLANT MODIFICATION(21,4)|EXTENSIN PROTEIN(21,3)|CARBONIC ANHYDRASE TRANSPORT(20,6)|BIOMOLECULE(20,5)|AGROBACTERIUM SP(20,3)|BREEDING PROGRAM(20,1)|ROOT EPIDERMIS(19,2)|SECRETION(18,5)|CARROT PLANT(18,3)|PROCESSING PLANT PRODUCTION(18,3)|GERMPLASM(18,1)|INCORPORATION(18,1)|PLANT CARBON SEQUESTRATION ABILITY(18,1)|ROOT TISSUE(17,4)|PROTEIN SECRETION PATHWAY(17,3)|BYPRODUCT(17,1)|ROOT CELL(16,58)|PROGENY(16,10)|EMBRYO(16,8)|CROP(16,4)|LEVINGTON ADVANCE F2S SEED(16,4)|PROMOTOR(16,4)|MEMBRANE ANCHORING SEQUENCE(16,3)|POLYPEPTIDE CODING DNA(16,3)|PLASMA MEMBRANE(15,22)|AGROBACTERIUM TUMEFASCIEN(15,5)|PLANT ROOT(14,41)|CO2 SEQUESTRATION(14,7)|PLANT ORGAN(14,7)|LEVINGTON M3 COMPOST(14,3)|HAZARDOUS WASTE(14,1)|ATMOSPHERIC CO2(13,9)|CODING SEQUENCE(13,9)|ANCHOR(13,6)|HERITABLE GENETIC MATERIAL ALTERING(13,6)|WASTE DISPOSAL(13,1)|PLANT CELL(12,28)|SEED(12,11)|CARBONIC ANHYDRASE ACTIVITY PROTEIN(12,7)|AGROBACTERIUM LB(11,6)|POLLEN GRAIN(11,6)|SECRET ABLE TRANSPORTABLE CARBONIC ANHYDRASE(11,5)|MICROPARTICLE(11,4)|ENDOGENOUS BASELINE EXPRESSION(11,3)|SOILS(11,2)|DIATOM CONTICRIBRA WEISSFLOGII(11,1)|TRANSMEMBRANE SEQUENCE(10,7)|TREE(10,7)|EUCALYPTUS(10,3)|FRUIT(10,3)|MELCOURT SHARP SAND(10,3)|MELCOURT TOPSOIL(10,3)|PLANT TISSUE(9,12)|CARBONIC ANHYDRASE ENZYMATIC ACTIVITY(9,6)|CARBONIC ANHYDRASE ENDOGENOUS LEVEL(9,4)|CROP PLANT(9,4)|EXPERIMENTALLY CHARACTERIZED SIGNAL PEPTIDE(9,4)|REPRESENTATIVE WORDING(9,4)|SAND COMPOST(9,4)|SECRETED PROTEIN(9,4)|ALFALFA(9,3)|CELL CULTURE(9,3)|CLOVER(9,3)|MILLET(9,3)|POPLAR(9,3)|SPRUCE(9,3)|SWEET POTATO(9,3)|GASEOUS CO2 INTERCONVERSION(9,2)|MATURE PLANT COMPOST(9,2)|ANNOTATED EUKARYOTIC CARBONIC ANHYDRASE(9,1)|FUNGUS ASPERGILLUS FICUUM(9,1)|GUS HISTOCHEMICAL STAINING(9,1)|HIGHLIGHT CYTOPLASMIC GFP EXPRESSION(9,1)|LONG TERM CO2 SEQUESTRATION(9,1)|RICE PLANT(9,1)|CO2 CONVERSION(8,7)|BICARBONATE ION(8,5)|HYDROPONIC BOX(8,5)|SOYBEAN PLANT ENGINEER(8,5)|CARBONIC ANHYDRASE INCREASED LEVEL(8,2)|CARBONIC ANHYDRASE SUBTYPE(8,2)|ENDOGENOUS CARBONIC ANHYDRASE(8,2)|PROCESSED PRODUCT(8,2)|ROOT SPECIFIC EXPRESSION(8,1)|SECRETED SOYBEAN CARBONIC ANHYDRASE(8,1)|HYDROPONIC SOLUTION(7,6)|ROOT CELL PROMOTER(7,6)|PERCENTAGE IDENTITY(7,4)|ATMOSPHERIC CO2 SEQUESTRATION(7,3)|BARLEY(7,3)|CALLUS CULTURE(7,3)|CANOLA(7,3)|CORN(7,3)|COTTON(7,3)|CRESS(7,3)|EXTRACELLULAR ENVIRONMENT CARBONIC ANHYDRASE(7,3)|GENE EXPRESSION REGULATORY ELEMENT(7,3)|GUS EXPRESSION(7,3)|NUCLEIC ACID SEQUENCE DETECTION(7,3)|PEA PLANT(7,3)|PINE(7,3)|SUGAR BEET(7,3)|TEFF(7,3)|TOMATO(7,3)|VETCH(7,3)|WHEAT(7,3)|DRIVING OVER EXPRESSION(7,2)|ICE CHILLED CO2(7,2)|MIRACLE GRO(7,2)|MODIFIED CARBONIC ANHYDRASE(7,2)|PLANT SELECTABLE MARKER(7,2)|SECRET ABLE CARBONIC ANHYDRASE(7,2)|SECRETED TRANSPORTED CARBONIC ANHYDRASE(7,2)|AGROBACTERIUM TUMEFACIENS MEDIATED TRANSFORMATION(7,1)|CARBONIC ANHYDRASE ENDOGENOUS EXPRESSION(7,1)|ENGINEERED ARABIDOPSIS THALIANA PLANT(7,1)|EXTRACELLULAR ROOT CARBONIC ANHYDRASE(7,1)|MEDIATED CO2 SEQUESTRATION(7,1)|MICROALGAE THALASSIOSIRA PSEUDONANA(7,1)|STAINED ARABIDOPSIS THALIANA ROOT(7,1)|TAGGED CARBONIC ANHYDRASE PROTEIN(7,1)|CRISPR(6,8)|TAILED STUDENT T TEST(6,8)|UNEQUAL VARIANCE(6,8)|AZYGOUS CONTROL PLANT(6,7)|CA PROTEIN(6,5)|DNA POLYNUCLEOTIDE SEQUENCE(6,4)|FRAGMENT FUNCTION(6,4)|ROOT EXTRACELLULAR ENVIRONMENT(6,4)|CONTAINED ENGINEERED PLANT(6,3)|EXPRESSION DOMAIN(6,3)|GLYCINE MAX(6,3)|GROUND BIOMASS(6,3)|RYE(6,3)|ARABIDOPSIS ROOT(6,2)|AZYGOUS PLANT(6,2)|COLORIMETRIC ASSAY(6,2)|CONCENTRATED HYDROPONIC MEDIA SAMPLE(6,2)|EXTRACELLULAR MEMBRANE(6,2)|EXTRACELLULAR ROOT ENVIRONMENT(6,2)|GENE REPORTER FUSION(6,2)|MULTICLONING SITE(6,2)|PERLITE SOIL(6,2)|SEQUESTERING CO2(6,2)|TARGETING PEPTIDE(6,2)|TRANSGENIC MANIPULATION(6,2)|TRANSPORT CARBONIC ANHYDRASE(6,2)|UNTRANSFORMED PLANT(6,2)|BACTERIAL SELECTABLE MARKER(6,1)|CARBONIC ANHYDRASE ESTERASE(6,1)|CARBONIC ANHYDRASE POLYPEPTIDE(6,1)|CARROT EXTENSIN(6,1)|CLEAR CYTOSOLIC LOCALIZATION(6,1)|CO2 SOIL FLUX EXPERIMENT(6,1)|DONOR REPAIR TEMPLATE(6,1)|ENGINEERED CARBONIC ANHYDRASE(6,1)|ENGINEERED SOYBEAN HAIRY ROOT(6,1)|EXOGENOUS POLYNUCLEOTIDE(6,1)|EXTRACELLULAR CARBONIC ANHYDRASE(6,1)|EXTRACELLULAR CO2 HYDRATION(6,1)|FUSION CARBONIC ANHYDRASE PROTEIN(6,1)|GUS STAINED ROOT(6,1)|HARNESSING CARBONIC ANHYDRASE(6,1)|INTRACELLULAR CARBONIC ANHYDRASE(6,1)|JOHN INNES CEREAL MIX(6,1)|ORGANISM SKELETAL TISSUE(6,1)|POLYNUCLEOTIDE CARBONIC ANHYDRASE(6,1)|POSITIVELY TRANSFORMED ROOT TISSUE(6,1)|PROTEIN NONCONVENTIONAL TRANSPORT(6,1)|RADIO TRACER ASSAY(6,1)|RNACOATED PARTICLE BOMBARDMENT(6,1)|SOYBEAN EXPANSIN GENE PROMOTER(6,1)|SOYBEAN PROTOPLAST CONFOCAL IMAGE(6,1)|SOYBEAN PROTOPLAST PLASMA MEMBRANE(6,1)|TRANSFECTED PROTOPLAST(6,1)|TRANSFORMED PLANT REGENERATION(6,1)|VISUAL REPORTER EXPRESSION(6,1)|ELECTROPORATION(5,6)|GENETICALLY ENGINEERED PLANT(5,6)|N TERMINUS(5,6)|CELL WALL(5,5)|HOMOLOGY(5,5)|BIOMASS PRODUCTION(5,3)|DIRECTING SECRETION TRANSPORT(5,3)|MEASURABLE DECREASE(5,3)|ORDINARY SKILL PERSON(5,3)|POSITIVE COLONY(5,3)|SHOW CARBONIC ANHYDRASE(5,3)|SOIL INORGANIC CARBON CONTENT(5,3)|DIAMETER SOIL SAMPLER PROBE(5,2)|ENGINEERED PLANT ROOT(5,2)|ENHANCE CO2 SEQUESTRATION(5,2)|GROWTH PHENOTYPE(5,2)|ME AGAR(5,2)|RECOMBINATION SITE(5,2)|SOIL SLURRY(5,2)|SYNTHETIC PROMOTER(5,2)|AEROPONIC GROWTH(5,1)|AGROBACTERIUM RHIZOGENE STRAIN(5,1)|AGROBACTERIUM STRAIN(5,1)|CARBONIC ANHYDRASE ASSAY(5,1)|CARBONIC ANHYDRASE DRIVING EXPRESSION(5,1)|CARBONIC ANHYDRASE MRNA(5,1)|CARBONIC ANHYDRASE VARIANT(5,1)|CHILLED PESTLE(5,1)|DIFFERING POLYNUCLEOTIDE PEPTIDE SEQUENCE(5,1)|ENCODED CARBONIC ANHYDRASE(5,1)|GENETICALLY ENGINEERED ARABIDOPSIS(5,1)|GRAM NEGATIVE BACTERIUM BURKHOLDERIA(5,1)|GUS STAINING BUFFER(5,1)|HANNATM SOIL PH TESTER(5,1)|HIGHLIGHT FLUORESCENT PROTEIN EXPRESSION(5,1)|HOMOGENIZED ROOT SAMPLE(5,1)|INDUCIBLE PROMOTER(5,1)|INTERESTING OPPORTUNITY(5,1)|LYSOSOMAL SECRETION(5,1)|METLER PH PROBE(5,1)|MICROALGAE SPECIES(5,1)|MONOMERIC SUBTYPE(5,1)|NATIVE CARBONIC ANHYDRASE SEQUENCE(5,1)|NONENGINEERED PLANT(5,1)|POLYSACCHARIDE ANCHOR(5,1)|SEA URCHIN LARVA(5,1)|SEQUESTRATION MAGNITUDE(5,1)|SIGNALING PEPTIDE(5,1)|SOYBEAN ROOT HAIR(5,1)|UNCONVENTIONAL SECRETORY PATHWAY(5,1)|WILDTYPE ROOT ENVIRONMENT(5,1)|WORD CARBONIC ANHYDRASE(5,1)|Y CARBONIC ANHYDRASE(5,1)|COVER CROP(4,7)|PLANT TRANSFORMATION VECTOR(4,7)|PROTON(4,4)|SPECTINOMYCIN(4,4)|SUPERNATANT(4,4)|GLYCOPROTEIN(4,3)|OIL PALM(4,3)|BASELINE COMPARISON(4,2)|CELL STRAINER(4,2)|CO2 TURN CATALYZED CONVERSION(4,2)|DISCERNIBLE DIFFERENCE(4,2)|EXTRACTION BUFFER(4,2)|HYDROPONIC MEDIUM SAMPLE(4,2)|MEMBRANE BOUND PROTEIN(4,2)|PLANT CELL GENOME(4,2)|WASHING(4,2)|5X ATMOSPHERIC CO2(4,1)|CARBONIC ANHYDRASE DETECTION(4,1)|CARBONIC ANHYDRASE PROTEIN PRODUCTION(4,1)|CARBONIC ANHYDRASE SECRETION TRANSPORT(4,1)|CASTOR BEAN CATALASE(4,1)|CELLULAR EXPORT(4,1)|CLONAL PROPAGATION(4,1)|CO2 SEQUESTRATION FACILITATION(4,1)|EXCESS HYDROPONIC MEDIA(4,1)|EXOGENOUS SOIL TREATMENT(4,1)|EXTRACELLULAR EXPRESSION(4,1)|EXTRACORPOREAL CO2 REMOVAL(4,1)|FLORAL DIPPING(4,1)|GENETICALLY ENGINEERED SOYBEAN ROOT(4,1)|HAIRY ROOT TRANSFORMATION(4,1)|HCO3 ENHANCED CONVERSION(4,1)|HORTICULTURAL PLANT(4,1)|HYDROPONIC GROWTH ENVIRONMENT(4,1)|LEADER PEPTIDE(4,1)|MEAN CARBONIC ANHYDRASE(4,1)|MITIGATE SOIL EROSION(4,1)|MWCO PROTEIN(4,1)|NA2EDTA H2O(4,1)|ONEVIEW CAMERA(4,1)|PLANT NODULE(4,1)|PNITROPHENOL ACETATE(4,1)|PRIME EDITING(4,1)|PROMOTER GUS FUSION(4,1)|PROTEIN CONCENTRATION(4,1)|PROTEIN SECRETORY PATHWAY(4,1)|RELEASING ENZYME(4,1)|REPORTER GENE FUSION(4,1)|SEEDLING ROOT(4,1)|SEMIAQUATIC PLANT(4,1)|SOIL GROWN PLANT(4,1)|SORGHUM RICE(4,1)|SOYBEAN TRANSFORMATION(4,1)|TARGETED NUCLEASE(4,1)|TRANSGENIC ROOT SAMPLE(4,1)|TRANSGENIC SOYBEAN PLANT(4,1)|TRANSIT PEPTIDE(4,1)|VIRAL TRANSFECTION(4,1)|WEED PEST MANAGEMENT(4,1)|HERBICIDE RESISTANCE(3,6)|GRNA(3,5)|SEQUENCE IDENTITY(3,5)|ABSORBANCE(3,3)|ACETONITRILE(3,3)|BIOFUEL(3,3)|CULTIVAR(3,3)|DAUCUS CAROTA(3,3)|ENHANCER(3,3)|FALLOW PERIOD(3,3)|GENETIC ENGINEERING(3,3)|INTERNAL ENVIRONMENT(3,3)|PISUM SATIVUM(3,3)|SPECTROPHOTOMETER PLATE READER(3,3)|TERMINATOR(3,3)|ARABLE LAND(3,2)|ASEXUAL REPRODUCTION(3,2)|BROMOTHYMOL BLUE(3,2)|CASSAVA VEIN MOSAIC VIRUS(3,2)|CONVERSION ENHANCEMENT(3,2)|EQUILIBRIUM(3,2)|FLOWERING(3,2)|FORESTRY(3,2)|INCREASED ACCUMULATION(3,2)|INCREASED CARBONIC ANHYDRASE(3,2)|INORGANIC SOIL CARBON(3,2)|KANAMYCIN(3,2)|MICROINJECTION(3,2)|P NITROPHENYL HYDROLYSIS(3,2)|PLANT PRODUCTION(3,2)|SAMPLE FILTRATION(3,2)|SOIL RESPIRATION(3,2)|TALE NUCLEASE(3,2)|TUBER(3,2)|ABSORPTION COMPOUND(3,1)|ACTIVE ENGINEERED PLANT(3,1)|AGROECOSYSTEM(3,1)|ANCESTOR CELL(3,1)|ANCHOR MOLECULE(3,1)|ANIMAL CONSUMPTION(3,1)|ANTHROPOGENIC GREENHOUSE GAS EMISSION(3,1)|BACKWARD REACTION(3,1)|BICARBONATE SALT(3,1)|BRASSICA OLERACEA(3,1)|CA NUCLEASE(3,1)|CALLUS TISSUE(3,1)|CARBONIC ANHYDRASE ADAPTATION(3,1)|CARBONIC ANHYDRASE CODING SEQUENCE(3,1)|CARBONIC ANHYDRASE ENZYME ACTIVITY(3,1)|CARBONIC ANHYDRASE INCREASED EXPRESSION(3,1)|CARBONIC ANHYDRASE SOLUTION(3,1)|CHOICE SPECIES(3,1)|CO2 DISSOLUTION(3,1)|CO2 ENHANCED CONVERSION(3,1)|CONFERRED GENE EXPRESSION(3,1)|CONTRIBUTOR(3,1)|CROP PLANT SPECIES(3,1)|CRUSHED ROCK SOIL TREATMENT(3,1)|CYTOPLASMIC LOCALIZED CONTROL(3,1)|DOUBLE STRANDED BREAK(3,1)|DRIED BIOMASS(3,1)|ENHANCED CO2 SEQUESTRATION(3,1)|ENTIRE GLYCOPHOSPHATIDYLINOSITOL(3,1)|ENZYME ACTIVITY ASSAY(3,1)|ENZYME DISTRIBUTION(3,1)|ENZYME SEQUENCE(3,1)|EX VIVO EX PLANT(3,1)|EXOSOME RELEASE(3,1)|EXPRESSION ENHANCEMENT(3,1)|FERTILIZER TREATMENT(3,1)|GASEOUS CARBON DIOXIDE INTERCONVERSION(3,1)|GENE EDITING PROTEIN(3,1)|GENETICALLY ENGINEERED SOYBEAN PLANT(3,1)|GENETICALLY ENHANCED PLANT(3,1)|GRAMNEGATIVE BACTERIA(3,1)|HARVEST ABLE SEED(3,1)|HOST GENOME(3,1)|HYDROPONIC CONDITION(3,1)|IMMEDIATE ENVIRONMENT(3,1)|INORGANIC CARBON SEQUESTRATION(3,1)|INORGANIC ION(3,1)|ISOLATED PROTEIN SAMPLE(3,1)|LIFE DOMAIN(3,1)|LOCALIZATION SEQUENCE(3,1)|MERISTEMATIC REGION(3,1)|MULTIMER FORMATION(3,1)|NATIVE REGULATORY SEQUENCE(3,1)|NATURALLY OCCURRING ENZYME(3,1)|NATURALLY OCCURRING PROMOTER(3,1)|NET CARBON SEQUESTRATION(3,1)|NUTRIENT CONTENT(3,1)|OBSERVABLE NEGATIVE(3,1)|PGMPIN2B PROMOTER CONTROL(3,1)|PLANT EXPRESSION VECTOR(3,1)|PLANT ROOT TISSUE(3,1)|POLYNUCLEOTIDE ISOLATION(3,1)|POLYPEPTIDE ISOLATION(3,1)|PRIMARY MESENCHYME CELL CALCIFICATION(3,1)|PROTEIN CONSTRUCT(3,1)|PROTOCOL ADAPTED VERSION(3,1)|RECORDING WINDOW(3,1)|REDUCING GLOBAL CO2 EMISSION(3,1)|RI PLASMID(3,1)|ROOT PROMOTER SEQUENCE(3,1)|ROOT SPECIFIC PROMOTER VARIANT(3,1)|ROOTSPECIFIC CELL(3,1)|SEA FLOOR(3,1)|SNAP LID MICROCENTRIFUGE TUBE(3,1)|SOIL CO2 SEQUESTRATION RATE(3,1)|SOYBEAN ROOT CELL(3,1)|STABLE TRANSFORMATION(3,1)|SUBCELLULAR LOCALIZATION(3,1)|TARGET PEPTIDE(3,1)|TARGET PLANT(3,1)|TEMPLATE SEQUENCE(3,1)|TERRESTRIAL ECOSYSTEM(3,1)|THALASSIOSIRA WEISSFLOGII(3,1)|TRISHCI SOLUTION(3,1)|UNMODIFIED PLANT(3,1)|UNQUALIFIED SENSE(3,1)|VEGETATIVE CYCLE(3,1)|WATER REVERSIBLE CONVERSION(3,1)|Y SUBTYPE(3,1)|WILD TYPE PLANT(2,10)|CARBONIC ANHYDRASE EXPRESSION(2,4)|FIVE FOLD(2,3)|LBA(2,3)|PLANT FOOD(2,3)|NONHOMOLOGOUS END JOINING REPAIR(2,2)|ACCESSION NUMBER GLYMA 19G(2,1)|ACCLIMATIZATION(2,1)|ADZUKI BEAN(2,1)|ANCHORAGE(2,1)|APOPTOSIS(2,1)|AQUEOUS ENVIRONMENT(2,1)|ARABLE FARMING(2,1)|ARCHAEA(2,1)|AVERAGE SKILL(2,1)|BASE EDITOR(2,1)|BASE SUBSTITUTION(2,1)|BETA GLUCURONIDASE(2,1)|BIOCHEMISTRY(2,1)|BIODIVERSITY(2,1)|BIOINFORMATICS(2,1)|BIOLISTIC(2,1)|BLEBBING(2,1)|BOTANY(2,1)|BROMOCRESOL PURPLE(2,1)|C4 PHOTOSYNTHESIS(2,1)|CARBONIC ANHYDRASE LEVEL(2,1)|CELL EXTRACELLULAR ENVIRONMENT(2,1)|CELL TARGET PROTEIN(2,1)|CHAMBER COVER(2,1)|CHLOROPHYL(2,1)|COLOR CHANGE(2,1)|COMBINED EFFORT(2,1)|CONFOCAL MICROSCOPE(2,1)|CONTROL ARABIDOPSIS THALIANA PLANT(2,1)|CONTROLLED BREEDING(2,1)| (WO2024/149976)|CLAIMS |1. A plant whose heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment.|2. A plant according to claim 1 , wherein the carbonic anhydrase is over-expressed in the extracellular environment of the root cells in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells.|3. A plant according to claim 1 or 2, wherein the gene encoding the transportable carbonic anhydrase protein further comprises a signal peptide sequence for directing transport of the carbonic anhydrase into the extracellular environment of the plant root.|4. A polynucleotide sequence comprising a sequence coding for a polypeptide sequence under the control of a suitable promoter, wherein the polypeptide sequence comprises a carbonic anhydrase sequence and a signal peptide sequence, wherein the promoter is active in plant roots and capable of driving overexpression of the carbonic anhydrase, the signal peptide sequence being capable of directing transport of the carbonic anhydrase into the extracellular environment of a plant root.|5. A plant according to claim 3 or a polynucleotide sequence according to claim 4, wherein the signal peptide sequence is either natively encoded or translationally fused to the carbonic anhydrase sequence to ensure transport of the carbonic anhydrase to the extracellular environment of the plant root.|6. A plant according to any of claims 1 to 3 or 5 or a polynucleotide sequence according to claims 4 or 5, wherein the signal peptide sequence for directing transport is derived from a secreted protein that is transported to the extracellular environment by a protein secretion pathway.|7. A plant according to any of claims 3, 5 or 6, or a polynucleotide sequence according to any of claims 4 to 6, wherein the signal peptide sequence is derived from the extensin protein, preferably wherein it is derived from a carrot plant or derived from the vacuolar sorting protein, preferably wherein it is derived from a pea plant.|8. A plant or polynucleotide according to any one of the preceding claims, wherein the promoter, and/or where present the signal peptide sequence, is/are derived from a gene from the same plant species or variety as the plant.|9. A plant or polynucleotide according to any one of preceding claims, wherein the promoter is root-specific, preferably root hair and/or root epidermis specific.|10. A plant or polynucleotide according to any one of preceding claims, wherein the carbonic anhydrase further comprises a transmembrane domain or a membrane anchor sequence.|11. A plant or polynucleotide according to any one of preceding claims, wherein the carbonic anhydrase is an a, (3, y, 5,q, 0 or i subtype carbonic anhydrase, preferably a monomer.|12. A plant according to any of claims 1 to 3, wherein the gene encoding a transportable carbonic anhydrase protein comprises SEQ ID NO: 1 or SEQ ID NO: 2 or a sequence having at least 65% identity to SEQ ID NO: 1 or SEQ ID NO: 2, optionally wherein the promotor comprises SEQ ID NO: 6 or SEQ ID NO: 7 or a sequence having at least 65% identity to SEQ ID NO: 6 or SEQ ID NO: 7.|13. A plant according to claim 3, wherein the gene encoding a transportable carbonic anhydrase protein comprises SEQ ID NO: 1 or SEQ ID NO: 2 or a sequence having at least 65% identity to SEQ ID NO: 1 or SEQ ID NO: 2, optionally wherein the promotor comprises SEQ ID NO: 6 or SEQ ID NO: 7 or|a sequence having at least 65% identity to SEQ ID NO: 6 or SEQ ID NO: 7; and wherein the signal peptide sequence comprises SEQ ID NO: 3 or SEQ ID NO: 4 or a sequence having at least 65% identity to SEQ ID NO: 3 or SEQ ID NO: 4. |14. A polypeptide sequence encoded by the polynucleotide of any one of claims 4 to 11.|15. A plant cell, cell line or progeny thereof comprising the polynucleotide sequence or polypeptide sequence of any of claims 4 to 11 or 14.|16. A plant, polynucleotide, polypeptide, cell, cell line or progeny according to any preceding claim, wherein the plant is a crop, preferably a row or cover crop, preferably selected from a corn, soybean, pea, cotton, canola, camelina, potato, tomato, sugar beet, cassava, sweet potato, alfalfa, wheat, barley, sorghum, oat, sorghum, millet, rye, teff, rice plant, or clover, cress, brassicas, vetch and prairie grasses.|17. A plant, polynucleotide, polypeptide, cell, cell line or progeny according to any one of claims 1 -15, wherein the plant is a tree, preferably wherein the tree is poplar, spruce, pine, eucalyptus, oil palm or rubber.|18. A plant, polypeptide, polynucleotide, cell, cell line or progeny according to any preceding claim, wherein more carbon is sequestered into the extracellular environment of the plant in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells.|19. A plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus, cell culture, pollen grain or seed, derived or obtained from the plant according to any of claims 15 to 18.|20. A vector comprising the polynucleotide sequence of any of claims 4 to 11 or 16 to 18, wherein the vector is optionally a plasmid.|21. A composition for transformation of plant cells comprising the polynucleotide of any one of claims 4 to 11 or 16 to 18, or the vector of claim 20; optionally comprising microparticles coated with said polynucleotide or said vector.|22. A bacterium comprising the polynucleotide of any one of claims 4 to 11 or 16 to 18, or the vector of claim 20; optionally wherein the bacterium is E coli. or Agrobacterium sp., more preferably A. tumefaciens.|23. A plant comprising the polynucleotide of any one of claims 4 to 11 or 16 to 18 stably integrated into the genome thereof; preferably heritably integrated into the genome thereof.|24. A method of producing a plant or seed, comprising the steps of:-|(d) providing the vector of claim 20; |(e) activating the promoter operably linked to the polypeptide coding DNA;|(f) optionally wherein the polypeptide is overexpressed in the extracellular environment of the cell in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells. |25. A method for increasing the capacity of a plant to sequester carbon in the soil, the method comprising altering the heritable genetic material of the plant such that a carbonic anhydrase protein is transported from the roots of the plant into the extracellular environment.|26. A method according to claim 25, wherein the altering of heritable genetic material comprises inserting at least one polynucleotide into the heritable genetic material of a plant cell.|27. A method according to claim 25, wherein the altering of heritable genetic material comprises genetically editing the heritable genetic material of a plant cell.|28. A processed plant product obtained from the plant or the plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus, cell culture, pollen grain or seed of any one of claims 1 to 3, 5 to 19 and/or 23; optionally wherein the processed product comprises a detectable nucleic acid sequence of (i) a transportable carbonic anhydrase downstream of a gene expression regulatory element active in at least some of the root cells of a plant, or (ii) at least a portion of a polynucleotide of any one of claims 4 to 11 or 16 to 18. (WO2024/149976)|[0001] CARBON SEQUESTRATION WITH TRANSGENIC PLANTS EXPRESSING CARBONIC ANHYDRASE | [0002] FIELD OF THE INVENTION | [0003] The present invention relates to the field of biotechnology, and more specifically to compositions and methods for enhancing sequestration of atmospheric CO2 in soils using plants. Genetically modified plants expressing enzymes to facilitate CO2 sequestration are provided, along with enzyme sequences and their use in various applications. The invention further concerns parts of such modified plants, such as plant cells, plant parts, plant organs, fruits, seeds, embryos, germplasm and processed plant products. | [0004] BACKGROUND | [0005] Anthropogenic greenhouse gas emissions have already caused an approximately 1 °C rise in global surface temperature over pre-industrial levels (Masson-Delmotte, 2018). Carbon dioxide (CO2) emissions have been the main contributor to this warming and efforts to meet the requirements of the Paris agreement to stay below 2°C, and ideally 1.5°C, to mitigate against the worst effects of climate change (Horowitz, 2016) will require the combined effort of reducing global CO2 emissions and the development of technologies that increase the sequestration of atmospheric CO2 (Masson-Delmotte, 2018). | [0006] SUMMARY OF INVENTION | [0007] The inventors have unexpectedly found that carbonic anhydrase genes expressed in root cells can enable CO2 sequestration, for example as bicarbonate, in the extracellular environment of the roots. In doing so, they have provided a solution to sequestration of atmospheric CO2 that is relevant for industrial biotechnology. Prior to the present invention, carbonic anhydrase genes have not been over-expressed in plant root cells, nor have carbonic anhydrase proteins been exported from plant root cells, nor have carbonic anhydrase proteins been over-expressed on the surface of plant root cells or in the extracellular environment. Thus, the approach used herein isnovel. Overall, the present invention achieves enhanced carbon sequestration from the atmosphere with no observable negative or deleterious anatomical, physiological, biochemical or developmental effects on modified plants. | [0008] The present invention provides a plant which comprises, or whose heritable genetic material comprises, a gene encoding a secretable/transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is secreted/transported from the roots of the plant into the extracellular environment. Therefore, the invention provides a plant in which the genetic material has been modified, the modification being such that the modified plants express carbonic anhydrase or a portion thereof, in at least some root cells of the plant. This expression in root cells is additional to any endogenous expression of carbonic anhydrase in the plant, in particular in the plant root where endogenous expression does not provide secretable/transportable carbonic anhydrase or any substantial carbonic anhydrase enzymatic activity in the extracellular environment of the plant root. | [0009] The expressed carbonic anhydrase may lead to increased levels of extracellular root carbonic anhydrase enzymatic activity, or in other words carbonic anhydrase enzymatic activity in the extracellular environment of the roots of the plant. The extracellular root environment may, for example, be the soil or any other location where a plant may germinate or grow or be cultivated including aeroponic and/or hydroponic growth environments. | [0010] Also provided herein is a plant wherein the carbonic anhydrase is over-expressed in the extracellular environment of the root cells in comparison to a plant which does not comprise, or whose heritable genetic material does not comprise, a gene encoding a secretable/transportable carbonic anhydrase protein under the control of a promoter active in root cells. | [0011] In addition or alternatively, provided herein is a plant wherein the heritable genetic material of the plant has been modified to contain a gene encoding a secretable/transportable carbonic anhydrase protein under the control of a promoter active in root cells. The genetic modification results in a carbonic anhydrase that isover-expressed in the extracellular environment of the plant root in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells or has not been altered. | [0012] In some embodiments, the gene encoding the secretable/transportable carbonic anhydrase protein further comprises a signal peptide sequence for directing secretion/transport of the carbonic anhydrase into the extracellular environment of the plant root. | [0013] Also provided herein is a polynucleotide sequence comprising a sequence coding for a polypeptide sequence under the control of a suitable promoter, wherein the polypeptide sequence comprises a carbonic anhydrase sequence and a signal peptide sequence, wherein the promoter is active in plant roots and capable of driving expression of the carbonic anhydrase in root cells, wherein the signal peptide sequence is capable of directing secretion/transport of the carbonic anhydrase into the extracellular environment of a plant root. The signal peptide sequence of any polynucleotide sequence disclosed herein may either be natively encoded or translationally fused to the carbonic anhydrase sequence to ensure secretion/transport of the carbonic anhydrase to the extracellular environment of the plant root. The signal peptide sequence for directing secretion/transport may be derived from any secreted protein that is transported to the extracellular environment by a protein secretion pathway. The signal peptide sequence may also be derived from the extensin protein, and in some embodiments it may be derived from a carrot plant or derived from the vacuolar sorting protein, or derived from a pea plant. | [0014] The carbonic anhydrase (including the polynucleotide encoding it or the peptide itself) is transportable and, in some embodiments, may be secreted or secretable. Additionally, in some embodiments the carbonic anhydrase may be attached to the outside of the cell or to the plasma membrane by a transmembrane domain, or a transmembrane helix, or a membrane anchor, or a glycosylphosphatidylinositol (GPI) anchor, or any other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell.The promoter, signal peptide sequence, or carbonic anhydrase of the polynucleotide or plant disclosed herein may be derived from a gene from the same plant species or variety as the plant in which it is expressed. The promoter may be root-specific, and in some embodiments it may be root hair and/or root epidermis specific. The expression domain of the promoter may also include other cells and tissues of the plant so long as the expression domain includes the root. | [0015] Also provided herein are carbonic anhydrases further comprising a transmembrane domain or a membrane anchor sequence. The carbonic anhydrase may be an a, (3, y, 5, q, 0, or i subtype carbonic anhydrase. In some embodiments it is a monomer. | [0016] Provided herein are polypeptide sequences encoded by the polynucleotide disclosed herein. A plant cell, cell line or progeny thereof comprising the polynucleotide sequence or polypeptide sequence disclosed herein are also provided. The progeny may be a progeny of the plant cell or a progeny of the cell line. | [0017] In some embodiments, the plant, polynucleotide, polypeptide, cell, cell line or progeny disclosed herein may derive from a plant wherein the plant is a crop. In some embodiments the plant is a row or cover crop. In some embodiments, the plant is selected from a corn, soybean, pea, cotton, canola, camelina, potato, tomato, sugar beet, cassava, sweet potato, alfalfa, wheat, barley, sorghum, oat, sorghum, millet, rye, teff, rice, or clover, cress, brassicas, vetch and prairie grasses. Additionally, the polynucleotide, polypeptide, cell, cell line or progeny disclosed herein may derive from a plant wherein the plant is a tree. In some embodiments wherein the tree is poplar, spruce, pine, eucalyptus, oil palm or rubber. | [0018] Also provided herein is the plant, polypeptide, polynucleotide, cell, cell line or progeny disclosed herein, where more carbon is sequestered into the extracellular environment of the plant in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells.Additionally provided is a plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus, cell culture, pollen grain or seed, derived or obtained from the plant disclosed herein. | [0019] Provided herein is a vector comprising the polynucleotide sequence disclosed herein. The vector is optionally a plasmid. Plasmids in accordance with the invention may further comprise one or more other elements selected from: an enhancer, a plant selectable marker, a multicloning site, or a recombination site. The structure, modification, propagation and generation of vectors or plasmids is well known to a person of ordinary skill in the art. | [0020] Also provided are compositions for transformation of plant cells comprising the polynucleotide, vector, or plasmid disclosed herein, optionally comprising microparticles coated with said polynucleotide or said vector. The microparticles may be of metal or synthetic material. In some embodiments the metal is tungsten or gold. | [0021] Also provided is a bacterium comprising the polynucleotide, plasmid, or vector disclosed herein, optionally wherein the bacterium is E coli. or Agrobacterium sp. In some embodiments the agrobacterium is A. tumefaciens. | [0022] Also provided herein are plants comprising the polynucleotide disclosed herein stably integrated into the genome thereof; and in some embodiments heritably integrated into the genome thereof. | [0023] Provided herein are methods of producing a plant or seed, comprising the steps of:- | [0024] (a) providing the vector or plasmid disclosed herein; | [0025] (b) activating the promoter operably linked to the polypeptide coding DNA;| [0026] (c) optionally wherein the polypeptide is overexpressed in the extracellular environment of the cell in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells.Methods for increasing the capacity of a plant to sequester carbon in the soil are also provided herein, the methods comprising altering the heritable genetic material of the plant such that a carbonic anhydrase protein is transported from the roots of the plant into the extracellular environment. The altering of heritable genetic material may comprise inserting at least one polynucleotide into the heritable genetic material of a plant cell. The altering of heritable genetic material may also comprise genetically editing the heritable genetic material of a plant cell. | [0027] A method in accordance with the invention may employ classical and well-known techniques of genetic modification, involving a method of transformation, whereby the polynucleotide of the invention is incorporated into a plant genome. Any necessary root cell expression regulatory elements may be present. In some embodiments this incorporation is stable and heritable so as to permit introduction of the modification into particular lines of crop plants; advantageously for the purposes of crop improvement or breeding programmes. A gene editing method may be used to incorporate or give rise to the polynucleotide of the invention. | [0028] Although various methods for gene editing are known, including TALE Nucleases (TALENs) or Zinc Fingers, a CRISPR system may also be used. For example a CRISPR-Cas system may be used whereby a guide RNA (gRNA) is selected to target the action of a CRISPR-Cas protein to a desired genomic locus resulting in a homologous recombination (HR) event or non-homologous end joining repair, i.e. insertion-deletion of the polynucleotide into the plant genome. | [0029] Therefore, the polynucleotide disclosed herein may include a polynucleotide encoding a CRISPR-Cas protein, optionally also a guide RNA (gRNA), wherein the gRNA directs the CRISPR-Cas protein to the locus of an endogenous carbonic anhydrase coding sequence in the plant cell genome, optionally wherein a regulatory element is inserted so as to cause expression of the carbonic anhydrase in at least some root cells of the plant. | [0030] Also provided herein are processed plant products obtained from the plant or the plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus culture, pollen grain or seed disclosed herein; optionally wherein the processed product comprises adetectable nucleic acid sequence of (i) a transportable carbonic anhydrase downstream of a gene expression regulatory element active in at least some of the root cells of a plant, or (ii) a polynucleotide or at least a portion of a polynucleotide disclosed herein. | [0031] BRIEF DESCRIPTION OF THE FIGURES | [0032] The invention will be further described by way of reference to the examples and accompanying figures. | [0033] Figure 1 depicts an illustrative diagram of the genetic vector used for soybean transformation to express a secreted-version of a soybean carbonic anhydrase in roots. | [0034] Figure 2 demonstrates that the carbonic anhydrase activity of the extracellular environment around the roots is enhanced in genetically engineered plants compared to wild type (control plants). A) shows carbonic anhydrase activity in a supernatant following enzyme liberation from root tissue of control and engineered soybean hairy roots. Standard error bars shown. B) shows carbonic anhydrase activity in the hydroponic solution in which control and genetically engineered plants were grown. Standard error bars shown. C) shows that genetically engineered plants produce a measurable decrease in soil pH relative to both soil-only control pots and control plants. This demonstrates that carbonic anhydrase has catalysed the conversion of CO2 in the air into bicarbonate and a proton in the soil. Standard error bars shown. D) shows that engineered plant roots sequester CO2 from the atmosphere, which control plant roots are not able to do. CO2 sequestration is shown for pots containing soil and plant roots (above ground tissue excised) over a 30-m inute measurement period. Standard error bars are shown. E) shows carbonic anhydrase activity in the extracellular environment of the roots of wild type and transgenic plants. This shows that transgenic plants have higher carbonic anhydrase activity. F) shows that there are no discernible differences in growth phenotype between control and genetically engineered Arabidopsis plants that secrete carbonic anhydrase from roots. Photo taken of 5-week-old control plant (left) and engineered plant of this invention (right). Scale bar represents 5cm.Figure 3 depicts a general schematic for the DNA sequence of the fusion carbonic anhydrase protein. Such constructs are typified by the inclusion of a genetic sequence encoding a protein with carbonic anhydrase activity, a promoter ensuring the sequence is expressed e.g. in plant root tissues, a terminator, and a peptide sequence designating cellular export e.g. an N-terminus signal peptide. | [0035] Figure 4 demonstrates that the carbonic anhydrase activity of the extracellular environment around the roots is enhanced in genetically engineered plants compared to wild type (control plants). A) shows that carbonic anhydrase activity in the hydroponic solution in which genetically engineered soybean plants that transport carbonic anhydrase from the roots of the plant into the extracellular environment were grown is higher relative to control plants. Standard error bars shown. B) shows that genetically engineered soybean plants that transport carbonic anhydrase from the roots of the plant into the extracellular environment produce a measurable decrease in soil pH relative to control plants. This demonstrates that carbonic anhydrase has catalysed the conversion of CO2 in the air into bicarbonate and a proton in the soil. Standard error bars shown. C) shows that genetically engineered soybean plants with carbonic anhydrase embedded on root surface produce a measurable decrease in soil pH relative to control plants. This demonstrates that carbonic anhydrase has catalysed the conversion of CO2 in the air into bicarbonate and a proton in the soil. Standard error bars shown. D) shows increased carbonic anhydrase activity in the hydroponic solution in which genetically engineered soybean plants with an alternative carbonic anhydrase were grown, relative to hydroponic solution in which control plants were grown. Standard error bars shown. E) demonstrates increased carbonic anhydrase activity from the roots of genetically engineered soybean plants relative to control plants. Standard error bars shown. F) shows that there are no discernible differences in growth phenotype between control and genetically engineered soybean plants that secrete carbonic anhydrase from roots. Photo taken of 5-week-old control plant (left) and engineered plant of this invention (right). Scale bar represents 5cm. | [0036] Figure 5 A+B: Confocal images of soybean protoplasts expressing fluorescent protein tagged carbonic anhydrase protein. A) Conticribra weissflogii carbonic anhydrase fused with a fluorescent protein. B) Conticribra weissflogii carbonic anhydrase fused with a fluorescent protein with the PsBP80 signal peptide at the N-terminus of thefusion protein and the PsBP80 transmembrane domain at the C-terminus of the fusion protein. C+D: Light microscope images of GUS stained Arabidopsis thaliana roots. C) GUS staining of Arabidopsis roots expressing GUS under the control of the pGmPIN2b promoter. D) GUS stain of Arabidopsis roots expressing GUS under the control of the pGmEXPA7 promoter. Scale bar represents: A) 10 pm, B) 20 pm, C) 50 pm, D) 50 pm. Arrows on A) highlight cytoplasmic GFP expression and B) highlight fluorescent protein expression localised to plasma membrane of the soybean protoplast. Arrows on C) left image and right image and D) left image, highlight areas of GUS stained root. | [0037] Figure 6 demonstrates carbonic anhydrase activity of the extracellular environment around the roots in genetically engineered plants enhanced inorganic carbon sequestration in soil compared to wild type (control plants) A) Analysis of soil inorganic carbon content demonstrating that the soil in which engineered soybean plants of this invention are grown accumulates more inorganic carbon compared to soil in which control soybean plants are grown and no plants are grown. B) shows that following treatment with hydrated lime Ca(OH)2, soil in which engineered Arabidopsis thaliana plants of the invention are grown accumulates more soil inorganic carbon than soil in which control Arabidopsis thaliana plants are grown. C) shows that the result shown in B is consistent when soil inorganic carbon content is normalised by soil organic carbon content. D) shows that soil in which engineered soybean plants of this invention are grown accumulates more soil inorganic carbon than soil in which control soybean plants are grown. E) shows that the result shown in D is consistent when soil inorganic carbon content is normalised by soil organic carbon content. | [0038] DETAILED DESCRIPTION | [0039] Weathering mediated CO2 sequestration | [0040] One way that CO2 is naturally sequestered from the atmosphere is through the process of chemical rock weathering. This occurs when atmospheric CO2 dissolves in rainwater to form carbonic acid (H2CO3). When carbonic acid encounters carbonate and/or silicate rock a chemical reaction occurs that causes the rock to breakdown and ions of bicarbonate (HCO3 ) and calcium (Ca2+) to be released. These ions are carriedby surface waters to the ocean where they precipitate out and fall to the ocean floor for long-term burial (i.e. hundreds of thousands of years). The ability of this process to facilitate long-term sequestration of atmospheric CO2 has led to the proposal of methods that accelerate the chemical rock weathering. These methods, known as enhanced weathering, involve substantially increasing the surface area of rock exposed to rain (containing dissolved CO2) by mechanically crushing it into dust and spreading it over terrestrial ecosystems. This has been proposed to greatly increases the rate at which rock is weathered, and thus the rate at which CO2 is sequestered from the atmosphere (Strefler et al., 2018). | [0041] Carbonic anhydrase | [0042] Carbonic anhydrases are a group of naturally occurring enzymes that catalyse the interconversion of gaseous carbon dioxide (CO2) and water (H2O) into ions of bicarbonate (HCO3 ) and hydrogen (H+) [CO2 + H2O HCOs” + H+], Carbonic anhydrase is a widely distributed enzyme, with members of this enzyme family found in organisms from across the tree of life, from bacteria and archaea to plants and animals. Given the activity of the enzyme there has been interest in using carbonic anhydrase enzymes in industrial settings to capture CO2 from industrial flue gas (as discussed in Boone et al., 2013 and Steger et al., 2022). WO 2015183935A2 also describes the use of modified carbonic anhydrases to catalyse the removal of CO2 from industrial flue gas. Also disclosed is the use of modified carbonic anhydrases which are affixed to a matrix and cross-linked with mineral ions so that a bicarbonate salt is precipitated out, thereby removing the CO2. This process is used in desalination and extracorporeal CO2 removal. Similarly, WO2013159228A1 describes an industrial process whereby CO2 is contacted with a carbonic anhydrase solution containing an additional absorption compound which together sequester the CO2. | [0043] Carbonic anhydrases (CAs) are metalloenzymes that contain a metal co-factor (typically Zn2+ but in some cases Cd2+, Co2+, Fe2+ and Mn2+ although one newly described class of carbonic anhydrase has been shown to exhibit activity under metal- free conditions (Hirakawa et al., 2021 )). To date, eight classes of carbonic anhydrases have been identified (a, (3, y, 5, q, 9, and i) with varying distribution across the three domains of life, a, (3, and y carbonic anhydrases are present in eukaryotes andprokaryotes, while other classes are found in some species of microalgae and protists. A recently described i-CA has been identified in the microalgae Thalassiosira pseudonana and the gram-negative bacterium Burkholderia territorii. Depending on the class, carbonic anhydrases may be active as monomers, dimers, trimers, tetramers, or octomers. In addition to their diversity in form, carbonic anhydrases have diverse functions between and within organisms. In plants, for example, carbonic anhydrases are present in several different plants tissues and vary in their subcellular localisation (DiMario et al., 2017). All carbonic anhydrases, irrespective of their class or the organism in which they are found, catalyse the same biochemical reaction, i.e. the interconversion of gaseous CO2 and water (H2O) into ions of bicarbonate (HCO3 ) and hydrogen ions (H+) as described above. | [0044] Recently, Matt et al. 2022 have described the expression of a glycosylphosphatidylinositol-anchored membrane-bound extracellular carbonic anhydrase in the calcifying primary mesenchyme cells of sea urchin larva. Extracellular CO2 hydration is demonstrated in these findings to suggest the resulting bicarbonate is taken up by the cell for the construction of carbonate structures that form the skeletal tissue of this organism. | [0045] Plants present an interesting opportunity for harnessing carbonic anhydrase for CO2 sequestration as bicarbonate in the soil and for the long-term sequestration of that bicarbonate via ground waters in an analogous manner to the chemical weathering process. Plant roots are in direct contact with the soil and with gaseous CO2 in the soil, which is itself in equilibrium with atmospheric CO2. | [0046] Historically, plants have been genetically engineered to express and secrete enzymes. Li et al. 2009 describes soybean plants which have been transformed with a construct containing a gene encoding a phytase from the fungus Aspergillus ficuum fused at the N-terminus with a signal peptide sequence from a carrot extensin gene. This recombinant gene was then fused to a promoter from the Arabidopsis Pky10 gene which conferred gene expression in the roots of the transgenic soybean plants. | [0047] Here we propose engineering plants to express in their root cells (specifically the outer cell layer, i.e. epidermal cells) an engineered form of carbonic anhydrase which issecreted from the cell into the extracellular environment. In particular, targeting plants which cover a large surface area of the globe (e.g., crop plant species) would provide a means by which atmospheric CO2 could be sequestered at large scale as bicarbonate ions in the soil. Following transport by surface waters, some of this bicarbonate is expected to be carried to, and buried in, the oceans. | [0048] Bioremediation denotes any process which employs a biological system (such as plants or bacteria) to remove environmental pollutants such as CO2 from natural or industrial settings. Bioremediation methods, such as that presented by the present invention, have particular advantages. Bioremediation often requires fewer resources and less energy than industrial man-made technologies and can be specifically altered through genetic engineering to address the specific needs of a particular environment. Additionally, these biological methods do not produce hazardous waste as byproducts, and therefore do not require expensive specialist waste disposal. | [0049] A need exists in the art to find ways to accelerate long-term CO2 sequestration by utilising bioremediation methods. Moreover, there is a need to achieve this through scalable methods that can be implemented rapidly and globally to urgently address the issue of anthropogenic CO2 release and elevated atmospheric CO2 concentration. The present invention addresses this need by demonstrating that expression of carbonic anhydrase in roots of plants, leading to increased levels of extracellular carbonic anhydrase enzymatic activity, results in enhanced CO2 sequestration through conversion of CO2 to bicarbonate. The present invention also demonstrates that multiple different natural or engineered carbonic anhydrase genes from different species can provide this function in plants. Unexpectedly, the inventors have found that this function can be provided when carbonic anhydrase proteins are secreted from plants, and/or when carbonic anhydrase proteins are anchored to the external periphery of the cell, either through for example a transmembrane domain or an anchor. Optionally, the N-terminus or C-terminus may be fused to a transmembrane domain, transmembrane helix, or a glycosylphosphatidylinositol (GPI) anchor, or other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. The present invention also demonstrates that carbonic anhydrase proteins in various compositional formsdescribed above can be expressed in plants using a variety of promoters that achieve the desired expression in root tissue. | [0050] The following detailed description conveys exemplary embodiments of the present invention in sufficient detail to enable those of ordinary skill in the art to practice the present invention. Features, or limitations of the various embodiments described do not necessarily limit other embodiments of the present invention, or the present invention as a whole. Hence the following detailed description does not limit the scope of the present invention, which is defined only by the claims. | [0051] Conventional techniques in botany, microbiology, tissue culture, molecular biology, chemistry, biochemistry and recombinant DNA technology and bioinformatics for use in employing the present invention are all readily known and available to a person of average skill in the art. Specific techniques are explained fully in the literature. | [0052] In the present specification the term “genetically engineered' is used and as will be familiar to a person of skill in the art this term may encompass the terms “genetically modified” and “gene editing”, each of which is appreciated in the art as having respectively differing meanings and underlying technical methodology. However, the term “modified” in an unqualified sense herein, may be understood more simply to mean “changed”, “altered” or “different”. The terms “altered”, “changed” and “modified” may be used interchangeably herein. The terms "increase", "improve" or "enhance" are used interchangeably herein. | [0053] The present invention provides a plant whose heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment. | [0054] The plant of the invention may be a genetically modified plant, a genetically enhanced plant, a non-naturally occurring plant and/or a genetically engineered plant. In some instances, the plant may be transgenic plant. | [0055] Plants in accordance with the invention may be monocots or dicots; in some embodiments they are crop plants, e.g. fruits, vegetables, cereals, oilseed, andlegumes, and may commonly be used for food, animal feed, biofuel or biomass production. A crop plant is any plant which is grown on a commercial scale for human or animal consumption or use. The plants may also be trees, particularly those popular in forestry and land management, carbon capture and biofuel or biomass production. The plants may be horticultural plants. In some embodiments, the plants are cover crops which are plants used to cover exposed soil between harvesting. Cover crops are utilised to mitigate soil erosion, increase soil fertility and quality, in the conservation of water, management of weeds/pests and diseases and to maintain biodiversity and wildlife in an agroecosystem. Cover crops may be utilized during a fallow period in arable farming. During a fallow period, arable land is not sown with harvestable seed for at least one or more vegetative cycles. This allows the arable land to recover. Cover crops may be sown during a fallow period to assist in the recovery of the land. | [0056] Heritable genetic material denotes any polynucleotide sequence and any associated genetic elements in any cell or organelle which is capable of being passed from one generation to a subsequent generation through sexual or asexual reproduction. Sexual plant breeding methods may include propagation. Asexual reproduction, also known as clonal propagation, by way of grafting plant cuttings is also considered as the incorporation of heritable genetic material into the genome of the plant. The heritable genetic material may therefore only be present in part of the plant. | [0057] The term “gene” denotes a polynucleotide sequence which codes for a polypeptide in full or in part comprising introns and exons, and an open reading frame (ORF) to enable transcription. The term code denotes the ability of a nucleotide sequence to act as a template for translation, whereby the arrangement of nucleotides represents codons which further represent amino acids. A gene may further comprise additional genetic elements such as a promoter, repressor, terminator, enhancer and/or transcription factor binding elements. A gene may be inserted into the genome of an organism using genetic engineering methods known in the art, such as transformation. A gene may be exogenous (i.e. not native, inserted into the existing genome) or endogenous (i.e. exists within the genome as a native gene). | [0058] The polypeptide of the invention may be a fusion protein. A fusion protein is a polypeptide which derives from a single nucleotide sequence which contains two ormore genes or portions of genes, wherein the genes code for separate polypeptides which would not natively be transcribed and translated together. | [0059] Typically, the polynucleotide of the invention comprises a promoter, a start codon, a sequence encoding an N terminal signal peptide, a sequence encoding a protein with carbonic anhydrase activity, optionally a sequence encoding a C terminus peptide which targets the polypeptide to a further specific location e.g. anchoring in the plasma membrane, a stop codon and a terminator, as typified in Figure 3. | [0060] The coding sequence of the carbonic anhydrase encoded in the DNA polynucleotide sequence of the invention may correspond to any of the polynucleotide sequences of SEQ ID NO: 1 , or SEQ ID NO: 2, or a sequence of at least 65% identity with any of said sequences; or a sequence of at least 70% identity with any of said sequences; or a sequence of at least 80% identity with any of said sequences, or at least 85%, at least 90%, or at least 95%, identity with any of said sequences. In some embodiments, the carbonic anhydrase will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity. | [0061] The amino acid sequence of the carbonic anhydrase encoded in the polynucleotide sequence(s) of the invention may correspond to any of the amino acid sequences of SEQ ID NO: 8, or SEQ ID NO: 9, or a sequence of at least 65% identity with any of said sequences; or a sequence of at least 70% identity with any of said sequences; or a sequence of at least 80% identity with any of said sequences, or at least 85%, at least 90%, or at least 95%, identity with any of said sequences. In some embodiments, the carbonic anhydrase will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity, preferably in the extracellular root environment. | [0062] The polynucleotide may correspond to a full-length carbonic anhydrase, or a portion thereof. The term “portion”, “variant”, “homolog” or other representative wording in the art as used herein used in relation to a carbonic anhydrase sequence, or a functional fragment thereof, means any carbonic anhydrase ortholog of a differing polynucleotide or polypeptide sequence from any species, including plants.In terms of percentage identity to a reference sequence, such as SEQ ID N0:1 , 2, 8 or 9 a variant of a carbonic anhydrase may have, in increasing order of preference, at least 65%, at least 66%, at least 67%, at least 68%, at least 69%, at least 70%, at least 71 %, at least 72%, at least at least 73%, at least 74%, at least 75%, at least 76%, at least 77%, at least 78%, at least 79%, at least 80%, at least 81 %, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91 %, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, or at least 99% overall sequence identity to that reference sequence. | [0063] Carbonic anhydrases are enzymes which catalyse the reversible conversion of water (H2O) and carbon dioxide (CO2) into bicarbonate (HCO3 ) and hydrogen (H+), as detailed below:- | [0064] H2O + CO2 « HCO3- + H+| [0065] In the absence of carbonic anhydrase enzyme activity the pH of the aqueous environment determines whether the forward or backward reaction is preferred. Carbonic anhydrases are widely distributed in all organisms. Carbonic anhydrases alter the rate at which this reaction occurs and the equilibrium between CO2 and HCOs' . Carbonic anhydrases from different species may have minimal sequence similarity but can adopt similar tertiary structures to catalyse this reaction in very different contexts. | [0066] In some embodiments, the carbonic anhydrase may be an a, (3, y, 5, q, 9, or i subtype carbonic anhydrase, and in some embodiments it is a monomer. Three classes of carbonic anhydrases natively exist in plants; a, [3 and y subtypes. The [3 subtypes are better characterised and include isoforms with high efficiency for CO2 hydration; for example, [3 subtypes function as part of C4 photosynthesis in C4 plants. [3 subtypes are dimeric, whilst a subtypes are monomeric. Monomeric subtypes have the advantage that there is no requirement for multimer formation at the surface of the cell.The carbonic anhydrase sequence used in this invention may be a homolog, analog, ortholog, or paralog of any subtype of carbonic anhydrase isolated from any species. It would be expected by a person of ordinary skill in the art that any carbonic anhydrase enzyme would work equivalently in this invention, so long as it was suitable for expression by the plants of the invention (for example it consisted of naturally occurring amino acids in protein form). The Examples of the present application demonstrate that sequence identity or similarity between carbonic anhydrases is not required in order for plants of the invention to exhibit their surprising ability to sequester CO2. As noted above, carbonic anhydrases from different species can adopt similar tertiary structures regardless of sequence similarity. The skilled person would therefore understand that a plant of the invention overexpressing any type of carbonic anhydrase in the extracellular environment of the root cells would function to sequester CO2. The skilled person understands carbonic anhydrases are defined by their function. As such, any enzyme that catalyses the interconversion of gaseous CO2 and water (H2O) into ions of bicarbonate (HCO3 ) and hydrogen ions (H+) is envisaged as a carbonic anhydrase protein as part of the invention. | [0067] In some embodiments, a carbonic anhydrase with high catalytic efficiency in the direction of bicarbonate formation is selected, such that the reverse reaction would not be favored. A carbonic anhydrase may be selected based on efficacy, for example, determined via an enzyme activity assay. In addition, codon usage may be altered to enhance expression for a particular plant species. | [0068] In some embodiments, in any aspect of the invention herein defined, the promoter is a root cell specific promoter (i.e. a root cell specific promoter, or a promoter that is expressed in root cells). A promoter active in root cells is a promoter which is presently enabling expression of a polynucleotide sequence in a root cell, i.e. it is sufficient for protein production in root cells. The promoter may be active in other cells of the plant, and in some embodiments comparatively greater in root cells. The activity of the promoter may be enhanced when compared to a wild-type promoter. The activity of the promoter may be conditionally enhanced. The promoter may be an inducible promoter. The activity of the promoter may vary, such as seasonally, diurnally or in response to an external signal, i.e. temperature, pH, nutrient content of the soil. The promoter may be constitutively active.The promoter may be a synthetic promoter comprised of various selected elements. For example, such a synthetic promoter may comprise root cell specific transcription factor binding element upstream of a promoter element. There may be two or more transcription factor binding elements which may be the same or different. A plurality of such transcription factor binding elements may serve to enhance the activity and/or specificity of the promoter in root cells. The promoter may be derived from non-plant organisms, such as the 35S promoter. | [0069] In other aspects, the root cell specific promoter may be derived from a gene that is expressed preferentially or specifically in root cell of plants and therefore is a naturally occurring promoter. The gene may be expressed in other plant cell types at endogenous levels. The promoter may be selected based on its predicted function in a particular species. A person of skill in the art is well aware of many root cell specific promoters. The root cell specific promoter may be active in some or all other plant cells at some expression level but be highly expressed in the roots. | [0070] The root specific promoter encoded in the DNA polynucleotide sequence of the invention may correspond to any of the polynucleotide sequences of SEQ ID NO: 6, or SEQ ID NO: 7, or a sequence of at least 65% identity with any of said sequences; in some embodiments a sequence of at least 70% identity with any of said sequences; and in some embodiments a sequence of at least 80% identity with any of said sequences, or at least 85%, at least 90%, at least 95%, identity with any of said sequences. In some embodiments, the encoded carbonic anhydrase will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity. | [0071] The polynucleotide may correspond to a full-length root specific promoter, or a portion thereof. As mentioned above, it would be expected by a person of ordinary skill in the art that any promoter active in the roots of plants would work equivalently in this invention. | [0072] The term “portion”, “variant”, “homolog” or other representative wording in the art as used herein used in relation to a root specific promoter sequence, or a functionalfragment thereof, means any root specific promoter ortholog of a differing polynucleotide or polypeptide sequence from any species, including plants. | [0073] In terms of percentage identity to a reference sequence, such as SEQ ID NO:6 or 7, a variant of a root specific promoter may have, in increasing order of preference, at least 65%, at least 66%, at least 67%, at least 68%, at least 69%, at least 70%, at least 71 %, at least 72%, at least at least 73%, at least 74%, at least 75%, at least 76%, at least 77%, at least 78%, at least 79%, at least 80%, at least 81 %, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91 %, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, or at least 99% overall sequence identity to that reference sequence. | [0074] In one embodiment a plant whose heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells is provided wherein the gene encoding a transportable carbonic anhydrase protein comprises SEQ ID NO: 1 or SEQ ID NO: 2 or a sequence having at least 65% identity to SEQ ID NO: 1 or SEQ ID NO: 2, optionally wherein the promotor comprises SEQ ID NO: 6 or SEQ ID NO: 7 or a sequence having at least 65% identity to SEQ ID NO: 6 or SEQ ID NO: 7. | [0075] In one embodiment a plant whose heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells is provided wherein the gene encoding a transportable carbonic anhydrase protein comprises SEQ ID NO: 1 or SEQ ID NO: 2 or a sequence having at least 65% identity to SEQ ID NO: 1 or SEQ ID NO: 2, optionally wherein the promotor comprises SEQ ID NO: 6 or SEQ ID NO: 7 or a sequence having at least 65% identity to SEQ ID NO: 6 or SEQ ID NO: 7; and wherein the signal peptide sequence comprises SEQ ID NO: 3 or SEQ ID NO: 4 or a sequence having at least 65% identity to SEQ ID NO: 3 or SEQ ID NO: 4. | [0076] The root cell specific promoter may be ubiquitously active in all plant cells at endogenous levels. Endogenous levels of carbonic anhydrase mRNA and full-length polypeptide are lower in cells which are not root cells. The expression level of carbonicanhydrase may exceed endogenous levels in any biological context whereby carbonic anhydrase is expressed. The biological context may be in response to a change in the environment. | [0077] The term secreted is used to describe the transport of a protein from the inside to the outside of a cell. It is used interchangeably with transported or exported. Thus a secretable/transportable carbonic anhydrase is capable of being secreted/transported to the extracellular environment. In some embodiments, the carbonic anhydrase is transported across the plasma membrane via the secretory pathway. Secretory pathways can be conventional or non-conventional. In some embodiments, the carbonic anhydrase is transported through the conventional secretory pathway, resulting in transport of the carbonic anhydrase across the cell membrane at the cell periphery. Non-conventional transport of proteins such as carbonic anhydrase can occur through one of four pathways; direct protein translocation across the plasma membrane through membrane transport proteins, lysosomal secretion, exosome release and blebbing. Transport of the carbonic anhydrase may be active or passive. A secreted protein such as the carbonic anhydrase of the invention is in some embodiments located to the plasma membrane (also known as the extracellular membrane) in a cell. The carbonic anhydrase may be in contact with the extracellular membrane via an extracellular matrix protein such as a glycoprotein, such as extensin, or via a polysaccharide. Suitable glycoprotein and polysaccharide anchors are well known in the art. The carbonic anhydrase may be in contact with the plasma membrane via a molecular anchor such as a transmembrane domain, transmembrane helix, or a glycosylphosphatidylinositol (GPI) anchor, or other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. The carbonic anhydrase may be in contact with the plasma membrane via part of the carbonic anhydrase polypeptide of the invention, wherein part of the polypeptide represents a transmembrane protein. There may be one or more transmembrane domains. The carbonic anhydrase may not be in contact with the plasma membrane. The secreted/transported carbonic anhydrase may be adjacent to the plasma membrane or within the extracellular environment in close proximity of the plasma membrane, such as within the cell wall region. The carbonic anhydrase may remain in close proximity to the plasma membrane, but beyond the cell wall region. In some embodiments, the carbonic anhydrase is secreted into theimmediate environment surrounding the roots, such as soil or alternative bedding medium, when the plant is present in such a medium. In some embodiments, the carbonic anhydrase is not secreted within a plant nodule. The carbonic anhydrase may continue to be secreted/transported in ex vivo/ex planta when the plant is separated from another part of itself, i.e. a cutting. The secreted/transported carbonic anhydrase may diffuse out into the extracellular environment or remain on the root surface once secreted. The carbonic anhydrase secreted from the root cells may diffuse to other tissue or cell extracellular environments, such as those adjacent to root cells. This may include any cell in close proximity with the roots or the rhizophere. | [0078] The carbonic anhydrase may be released from the cell via a non-secretable pathway, such as apoptosis, or any physical interference with the cell membrane which exposes intracellular carbonic anhydrase to the extracellular environment. | [0079] The carbonic anhydrase may be over-expressed in the extracellular environment of the root cells in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells. | [0080] The term “over-expressed” regarding carbonic anhydrase refers to the expression level of carbonic anhydrase protein produced in comparison to endogenous baseline expression. The term “produced” is understood to refer to the production of the carbonic anhydrase protein and may be used interchangeably with the term expressed. Plants whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells will exhibit endogenous levels of carbonic anhydrase in all biological contexts and these levels of carbonic anhydrase will be used as a baseline comparison for the plants of the invention. Baseline levels of carbonic anhydrase typically reflect endogenous levels of carbonic anhydrases which may fluctuate according to the internal and external environment of a plant. Increased levels of carbonic anhydrase, i.e. any amount above baseline, will be considered to denote over-expression of the carbonic anhydrase protein. In some embodiments, the plant of the invention expresses 0.005%, 0.1 %, 0.5%, 1 %, 2%, 3%, 4%, 5%, 10%, 25%, 50%, 75%, 100%or 200% additional carbonic anhydrase protein in comparison to endogenous baseline expression. Endogenous baseline expression may be established in a control plant which may be a wild-type plant. Cells of the same type and morphology in the same location of the plant, i.e. root cells should be compared to one another. | [0081] A plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells is a plant which lacks a gene in its genome which encodes for a transportable carbonic anhydrase protein under the control of a promoter which is active in root cells. This plant has not been modified in the same fashion as the plants of the invention. This plant may be known as an untransformed plant, compared to a transformed plant of the invention. The plant may comprise other genetically modified elements related to or unrelated to carbonic anhydrases which are distinct from those of the invention. A plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells may be referred to or used as a “control” plant. Accordingly, the control plant has not been genetically modified to alter expression of the polynucleotide and/or polypeptide disclosed herein. This plant will exhibit endogenous levels of carbonic anhydrase in all biological contexts and these levels of carbonic anhydrase will be used as a baseline comparison for the plants of the invention. Baseline levels of carbonic anhydrase typically reflect endogenous levels of carbonic anhydrases which may fluctuate according to the internal and external environment of a plant. A control plant may be a wild-type plant. A control plant may be a wild-type plant of the same species as the plant of the invention. The control plant function is to provide a reliable reference against which the expression of polynucleotides or polypeptides of the invention can be compared against in a modified plant material. The plant of the invention may therefore be genetically engineered compared to a non-engineered plant. The control plant may be defined by determining the level of carbonic anhydrase activity by enzyme assays known in the art and defined herein. Carbonic anhydrase activity may be undetectable or at very low levels in a control plant when compared with the plant of the invention. A plant of the invention exhibits increased levels of carbonic anhydrase activity, i.e. any amount above of increased activity as compared to a control plant. Typically, a more than two-fold increase in carbonic anhydrase activity is observed in the plant of the invention compared to a control or unmodifiedplant. In some embodiments, the plant of the invention has more than a two-fold, threefold, four-fold or five-fold increase in carbonic anhydrase activity compared to a control plant. In some embodiments, the plant of the invention has more than a 0.005%, 0.1 %, 0.5%, 1 %, 2%, 3%, 4%, 5%, 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90% or 100% increase in carbonic anhydrase activity compared to a control plant. The carbonic anhydrase activity may be measured in the root cells, the whole root or whole plant. In some embodiments, the plant of the invention has more than a two-fold, threefold, four-fold or five-fold increase in carbonic anhydrase activity in the extracellular space compared to a control plant. In some embodiments, the carbonic anhydrase activity is quantified using the Wilbur-Anderson Units (WA) equation, or carbonic anhydrase esterase activity measured by the rate to catalyze hydrolysis of p- Nitrophenol acetate (pNPA) to known concentration of p-Nitrophenol (pNP) per unit of time which can alternatively be expressed in enzyme activity units such as katal (kat) or international units (IU), or carbonic anhydrase activity measured by units of conductivity changed per unit time, or carbonic anhydrase activity quantified using radiotracer based assays where activity is reported in counts or disintegrations per unit of time, or other equivalent methods to quantify carbonic anhydrase activity which is well understood by the skilled person. Optionally, the plant of the invention has a two-fold, three-fold, four-fold or five-fold increase in carbonic anhydrase activity in WA units compared to a control plant. | [0082] The gene encoding the transportable carbonic anhydrase protein may further comprise a signal peptide sequence for directing transport of the carbonic anhydrase into the extracellular environment of the plant root. The term “signal peptide” may also be known as a signal sequence, targeting signal, localization signal, localization sequence, transit peptide, target peptide, leader sequence or leader peptide. The signal peptide is usually present at the N-terminal of a polypeptide but may be present at the C-terminus. In the present invention, the signal peptide is present at the N-terminus. | [0083] Membrane-bound proteins can be type I or II; type I membrane-bound proteins rely on a signal peptide which directs them towards the secretory pathway which is subsequently cleaved, whereas type II proteins are targeted to the secretory pathwayvia their first transmembrane domain, which is not cleaved. Therefore, the signal peptide of the invention may or may not include a transmembrane domain. | [0084] The signal peptide sequence encoded in the DNA polynucleotide sequence of the invention may correspond to any of the polynucleotide sequences of SEQ ID NO: 3, or SEQ ID NO: 4, or a sequence of at least 65% identity with any of said sequences; in some embodiments a sequence of at least 70% identity with any of said sequences; and in some embodiments a sequence of at least 80% identity with any of said sequences, or at least 85%, at least 90%, at least 95%, identity with any of said sequences. In some embodiments, the carbonic anhydrase encoded from the above DNA sequences will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity. | [0085] The polynucleotide may correspond to a full length signal peptide, or a portion thereof. | [0086] The term “portion”, “variant”, “homolog” or other representative wording in the art as used herein used in relation to a signal peptide sequence, or a functional fragment thereof, means any signal peptide sequence of a differing polynucleotide or polypeptide sequence from any species, including plants. | [0087] In terms of percentage identity to a reference sequence, such as SEQ ID NO:3 or 4, a variant of a signal peptide sequence may have, in increasing order of preference, at least 65%, at least 66%, at least 67%, at least 68%, at least 69%, at least 70%, at least 71 %, at least 72%, at least at least 73%, at least 74%, at least 75%, at least 76%, at least 77%, at least 78%, at least 79%, at least 80%, at least 81 %, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91 %, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, or at least 99% overall sequence identity to that reference sequence. | [0088] The signal peptide sequence cooperates with the promoter to ensure extracellular expression and transport of the polypeptide sequence to the extracellular environment. | [0089] Also provided herein is a polynucleotide sequence comprising:• a suitable promoter; | [0090] • a sequence coding for a polypeptide sequence under the control of said suitable promoter; and | [0091] • a sequence encoding a signal peptide sequence; wherein the polypeptide sequence comprises a carbonic anhydrase sequence, and wherein the promoter is active in plant roots and capable of driving overexpression of the carbonic anhydrase, the signal peptide sequence being capable (prior to removal) of directing transport of the carbonic anhydrase into the extracellular environment of a plant root. | [0092] A suitable promoter is a promoter which enables the expression of a polypeptide sequence to which it is associated. The signal peptide sequence is sufficient to enable transport of the carbonic anhydrase into the extracellular environment of a plant root. | [0093] The signal peptide sequence may either be natively encoded or translationally fused to the carbonic anhydrase sequence to ensure transport of the carbonic anhydrase to the extracellular environment of the plant root. | [0094] The signal peptide sequence for directing transport may be derived from a secreted protein that is transported to the extracellular environment by a protein secretion pathway, and in some embodiments the conventional (or canonical) protein secretory pathway. The signal peptide sequence may be derived from the extensin protein, and in some embodiments it is derived from a carrot plant or derived from the vacuolar sorting protein, or it may be derived from a pea plant. | [0095] The plant or polynucleotide according to the invention may have a promoter, and/or a signal peptide sequence derived from a gene from the same plant species or variety as the plant. The plant or polynucleotide according to the invention may have a promoter and/or a signal peptide sequence derived from a gene from a different plant species, cultivar or variety as the plant. Plant varieties are genetic variations of the same species of plant which arise naturally in the environment. Cultivars are genetic variations of the same species of plant which have been develop by humans through controlled breeding.The promoter sequence, signal peptide sequence, transmembrane sequence and any other sequences present in the polynucleotide may be derived from any species, variety or cultivar. | [0096] The promoter of the invention is active in plant tissues that function as roots, and in some embodiments may be root hair cell and/or root epidermal cell specific. Rootspecific cells are those cells part of the root system of a plant, which may function in a root specific capacity, i.e. anchorage, stability, shelter, nutrient harvesting and storage, water absorption, transport of macromolecules. Underground stems (such as tubers, rhizomes, bulbs, corms, stolons, taro and other plant associated organs which reside underground near the roots) provide similar subterranean functions to botanically-defined root tissues and for the purposes of this invention may be considered as plant tissues that function as roots and comprise root cells. | [0097] The carbonic anhydrase may further comprise a transmembrane domain and/or a membrane anchor sequence. The transmembrane domain sequence may be a full length transmembrane domain sequence or a portion thereof. The transmembrane sequence may encode a transmembrane domain which is partially present in the plasma membrane once transported, or it may span the entire plasma membrane. The transmembrane sequence may comprise post-translational elements such as glycoproteins and polysaccharide structures. In some embodiments, the carbonic anhydrase may be attached to the outside of the cell or to the plasma membrane by a transmembrane domain, or a transmembrane helix, or a membrane anchor, or a glycosylphosphatidylinositol (GPI) anchor, or any other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. | [0098] In some embodiments, the transmembrane domain is derived from Pisum sativum BP80. The transmembrane domain sequence encoded in the DNA polynucleotide sequence of the invention may correspond to polynucleotide sequence SEQ ID NO: 5., or a sequence of at least 65% identity with any of said sequences; in some embodiments a sequence of at least 70% identity with any of said sequences; and in some embodiments a sequence of at least 80% identity with any of said sequences orat least 85%, at least 90%, at least 95%, identity with any of said sequences. In some embodiments, the carbonic anhydrase will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity. | [0099] The polynucleotide may correspond to a full-length transmembrane sequence, or a portion thereof. Additionally, the polynucleotide may comprise a sequence that is capable of directing the formation of a glycosylphosphatidylinositol (GPI) anchor, or any other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. | [0100] The term “portion”, “variant”, “homolog” or other representative wording in the art as used herein used in relation to a transmembrane sequence, or a functional fragment thereof, means any transmembrane sequence ortholog of a differing polynucleotide or polypeptide sequence from any species, including plants. | [0101] In terms of percentage identity to a reference sequence, such as SEQ ID NO:5, a variant of a transmembrane sequence may have, in increasing order of preference, at least 65%, at least 66%, at least 67%, at least 68%, at least 69%, at least 70%, at least 71 %, at least 72%, at least at least 73%, at least 74%, at least 75%, at least 76%, at least 77%, at least 78%, at least 79%, at least 80%, at least 81 %, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91 %, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, or at least 99% overall sequence identity to that reference sequence. | [0102] In some embodiments, the membrane anchor sequence corresponds to an entire glycophosphatidylinositol anchor sequence, or a portion thereof. | [0103] Also provided herein is an isolated polynucleotide sequence of the invention which may be fused to another polynucleotide sequence or to a targeting peptide sequence or to a transmembrane domain sequence. The polynucleotide may also be described as being engineered or non-naturally occurring.Also provided herein is an isolated polypeptide of the invention which may be fused to another polypeptide or to a targeting peptide or to a transmembrane domain. An isolated polynucleotide or polypeptide is a DNA or protein construct which exists on its own separate from the internal environment of the cell. These may comprise DNA or protein associated elements. These can be recombinant. The polypeptide of the invention may transiently comprise a signal peptide, which is subsequently cleaved upon entering the secretory pathway. The polypeptide of the invention may also comprise a signal peptide which represents a first transmembrane domain which acts as a signal peptide, which is not cleaved upon entering the secretory pathway. | [0104] Also provided herein are plant cells, cell lines or progeny thereof comprising the polynucleotide sequence or polypeptide sequence disclosed herein. The term “plant” encompasses whole plants, ancestors and progeny of the plants and plant parts, including seeds, fruit, shoots, stems, leaves, roots (including tubers), flowers, and tissues and organs, wherein each comprise the polynucleotide of the invention. The term "plant" also encompasses plant cells, suspension cultures, callus tissue, embryos, meristematic regions, gametophytes, sporophytes, pollen and microspores, wherein each comprise the polynucleotide of the invention. | [0105] In some embodiments, the plant is a crop, and in some embodiments a row or cover crop. In some embodiments the plant is selected from a corn, soybean, fava bean, mung bean, adzuki bean, broad bean, pea, cowpea, cotton, canola, camelina, potato, tomato, sugar beet, cassava, yam, sweet potato, alfalfa, wheat, barley, sorghum, oat, sorghum, millet, rye, teff, triticale, miscanthus, sorghum rice, or clover, cress, brassicas (such as Brassica oleracea), vetch and prairie grasses (such as switchgrass). | [0106] The plant may be a tree. In some embodiments the tree is poplar, spruce, pine, eucalyptus, oil palm or rubber, particularly those popular in forestry and land management, food production, carbon capture and biofuel or biomass production. | [0107] The plant may be an aquatic or a semi-aquatic plant. In some embodiments, such plants may be duckweed, mangroves, nymphaeales, or rice.The plant, polypeptide, polynucleotide, cell, cell line or progeny of the invention may sequester more carbon into the extracellular environment of the plant in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells. Sequestration of carbon occurs via the conversion of CO2 into bicarbonate and hydrogen ions. | [0108] Also provided herein are plant parts, plant tissues, plant organs, plant cells, plant protoplasts, embryos, callus cultures, pollen grains or seeds, derived or obtained from the plant of the invention. | [0109] Also provided herein are vectors comprising the polynucleotide sequence of the invention. In some embodiments, the vector is a plasmid. The plasmid may comprise an origin of replication, a T-DNA right border repeat of a Ti or Ri plasmid, a left border repeat of a Ti or Ri plasmid and at least one bacterial selectable marker. The plasmid may also comprise an enhancer, a plant selectable marker, a multicloning site and/or a recombination site. | [0110] Compositions for transformation of plant cells comprising the polynucleotide of the invention or the vector comprising the polynucleotide of the invention are also provided herein. The vector may comprise microparticles coated with said polynucleotide or said vector. | [0111] Transformation of plants is a routine technique in many species. Any of several transformation methods may be used to introduce a gene of interest into a suitable ancestor cell. According to the various aspects of the invention, the polynucleotide of the invention is introduced into a plant and expressed as a transgene through transformation. The term "introduction" or "transformation" as referred to herein encompasses the transfer of an exogenous polynucleotide into a host cell, irrespective of the method used for transfer. The methods described for the transformation and regeneration of plants from plant tissues or plant cells may be utilized for transient or for stable transformation. Transformation methods include the use of liposomes, electroporation, chemicals that increase free DNA uptake, injection of the DNA directly into the plant, floral dipping, biolistics, transformation using viruses or pollen andmicroinjection. Methods may be selected from electroporation, microinjection, RNA- coated particle bombardment or viral transfection, but are not limited to those methods recited here. The transformation method is usually dependent on the species of choice. The polynucleotide may be transiently or stably introduced into a host cell and may be maintained non-integrated, for example, as a plasmid. Alternatively, it may be integrated into the host genome. The resulting transformed plant cell may then be used to regenerate a transformed plant. To select transformed plants, plant material obtained in the transformation is, as a rule, subjected to selective conditions so that transformed plants can be distinguished from untransformed plants. For example, seeds obtained in the above-described manner can be planted and, after an initial growing period, subjected to a suitable selection and screening. | [0112] Also provided herein are bacteria comprising the polynucleotide of the invention, or a vector comprising the polynucleotide of the invention. In some embodiments, the bacterium is E coli. or Agrobacterium sp., and in some embodiments A. tumefaciens. Any suitable cloning system may be used. Genetically modified plants, including crop plants, are in some embodiments produced via Agrobacterium tumefaciens mediated transformation. Such routine methods are also used to introduce gene editing proteins such as CRISPR-Cas nucleases and base editors, which can be used to edit native carbonic anhydrase sequences to be transportable and be increased in expression in root cells. | [0113] Also provided herein are plants comprising the polynucleotide of the invention whereby the polynucleotide is stably integrated into the genome thereof; and in some embodiments heritably integrated into the genome thereof. | [0114] Methods of producing the plant or seed of the invention are also provided, comprising the steps of:- | [0115] (a) providing a vector comprising the polynucleotide of the invention; | [0116] (b) activating the promoter operably linked to the polypeptide coding DNA;| [0117] (c) optionally wherein the polypeptide is overexpressed in the extracellular environment of the cell in comparison to a plant whose heritable geneticmaterial does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells. | [0118] A method for increasing the capacity of a plant to sequester carbon in the soil, the method comprising altering the heritable genetic material of the plant such that a carbonic anhydrase protein is transported from the roots of the plant into the extracellular environment is also provided. The normal capacity of a plant to sequester carbon in the soil is indicated by a plant which has not been genetically modified in the same way as a plant of the present invention. This capacity may reflect the uppermost limit of the rate of conversion of CO2 into bicarbonate and hydrogen ions in the extracellular environment of plants which have not been genetically modified in the same way as a plant of the present invention. This rate achieved in the modified plants is inherently dependent upon the transport of carbonic anhydrase from the roots of the plant into the extracellular environment. The altering of heritable genetic material may comprise inserting at least one polynucleotide into the heritable genetic material of a plant cell using methods of transgenic manipulation is well known in the art. | [0119] The altering of heritable genetic material may also comprises genetically editing the heritable genetic material of a plant cell, using methods of genetic modification well known in the art, such as CRISPR, TALENs and meganucleases. Base editing may also be used, whereby a single nucleotide can be manipulated in a targeted gene. Prime editing may also be used, which is a search-and-replace genome editing method used to insert precise, small indels including single or multiple base substitutions, transitions and transversions without requiring double stranded breaks and donor repair templates. Any regulatory sequence may also be manipulated using these techniques to result in increased expression of the carbonic anhydrase, for example, by introducing random indels into a native regulatory sequence using a CRISPR-Cas system. | [0120] Any polynucleotides disclosed herein may further include a polynucleotide sequence encoding a CRISPR-Cas protein, optionally a guide RNA (gRNA), wherein the gRNA directs the CRISPR-Cas protein to the locus of at least one copy of an endogenous carbonic anhydrase gene thereof in the plant cell genome, whereby a root-specificpromoter is inserted so as to cause expression of the copy or copies of the carbonic anhydrase in at least some root cells of the plant. | [0121] A native carbonic anhydrase may also be manipulated using gene editing tools to introduce a signal peptide to a native carbonic anhydrase gene using targeted nucleases and homology directed repair or non-homologous end joining repair mechanisms and a template sequence containing the signalling peptide. Such gene knock in techniques are well known in the art. Also provided herein are processed plant products obtained from the plant or the plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus culture, pollen grain or seed disclosed herein. The processed plant product may comprise a detectable nucleic acid sequence of (i) a transportable carbonic anhydrase downstream of a gene expression regulatory element active in at least some of the root cells of a plant, or (ii) a polynucleotide or at least a portion of a polynucleotide of the invention which is present in the product. Processing may involve chemical or physical manipulation of the product in order to form a product with desirable properties suited to a particular function, i.e. pelleting.| [0122] EXAMPLES | [0123] Example 1 | [0124] To demonstrate that plant roots can be engineered to produce active carbonic anhydrase protein a soybean (Glycine max) carbonic anhydrase gene was selected for overexpression (accession number Glyma.19G135900 [SEQ ID NO: 1 and SEQ ID NO: 8]). This carbonic anhydrase has an annotated ‘Eukaryotic-type carbonic anhydrase’ domain (Pfam #PF00194.24) in its protein sequence. | [0125] The expression of the carbonic anhydrase gene (SEQ ID NO: 1 and SEQ ID NO: 8) was placed under the control of a 35S promoter and cloned into the pCAM BIA-1300 plant expression vector. This vector included a herbicide resistance gene (kanamycin) and the expression cassette was flanked by agrobacterium LB and RB t-DNA sequences. The vector was transformed into Agrobacterium rhizogenes strain K599 using electroporation and this was used to transform soybean roots using a hairy root transformation method according to the protocols in (Chen et al., 2018). | [0126] Following transformation positively transformed root tissue was identified visually by the expression of a visual reporter. Root tissue was isolated from transformed roots and equivalent non-transformed root tissue was sampled as a control. Root tissue was homogenised in in 700pl of extraction buffer in a chilled pestle and mortar. Homogenised root was transferred to 2ml tube and centrifuged for 15mins at 5000rpm at 4C. All assays were performed on the supernatant following this spin step. | [0127] A carbonic anhydrase assay was carried out to measure carbonic anhydrase activity. This assay measures the rate of change in pH of CO2-saturated water following the addition of root homogenate from transformed and untransformed (also known as wild type control) root tissue. The pH change results from the release of protons (H+) by carbonic anhydrase. Change in pH is directly proportional to the amount of bicarbonate that has been produced by carbonic anhydrase. Such assays are known to those familiar with the art. | [0128] For each carbonic anhydrase assay 10OpI of supernatant from the homogenised root samples was used. For a no-root tissue control, 1 OOpI of extraction buffer without roottissue was used. Samples were added to 2ml tube containing 1100pl of a 20 mM Tris- HCI solution at pH 8.3 containing 0.003% bromothymol blue. Following this, 800pl of ice chilled CO2 saturated water was added. The time taken to change colour from blue (pH 8.3) to yellow (pH 5.3) was recorded. All reactions were performed on ice. | [0129] The Wilbur-Anderson Units (WA) equation was used to calculate activity: | [0130] WA units = (tO-ts)Zts where to is the time taken for the colour change to occur in the no-root control reaction and fs is the time taken for the colour change to occur in samples containing supernatant from the homogenised root. | [0131] Carbonic anhydrase activity was significantly increased at ~2x higher in the transgenic root samples compared to the wild type root samples (P=0.022669, one-tailed Student’s t-test, unequal variance) (Figure 2A). Thus, soybean root cells can be engineered to have increased carbonic anhydrase activity through the overexpression of a gene encoding a carbonic anhydrase protein, and this protein is catalytically active when released from root cells into an extracellular environment. | [0132] Example 2 | [0133] In order for carbonic anhydrase to facilitate conversion of CO2 to HCO3 in the extracellular environment of the plant they need to be secreted/transported from the cells of the plant into the extracellular environment. There are several mechanisms by which cells target proteins for secretion/transport from the cell into the extracellular environment. The two main ways in which this is achieved are the conventional secretory pathway and the unconventional secretory pathway. The conventional secretory pathway achieves protein secretion/transport through the use of N-terminal signal peptides. | [0134] To demonstrate that carbonic anhydrase proteins can be engineered to be secreted/transported from plant cells we translationally fused an experimentally characterised signal peptide from the carrot (Daucus carota) extensin gene (G. Li et al., 2009) [SEQ ID NO: 3] with the soybean carbonic anhydrase provided in Example1 [SEQ ID NO: 1 and SEQ ID NO: 8], This fusion protein was placed under the control of a root specific promoter from the soybean expansin gene (Glyma.17G133100) [SEQ ID NO:6], and cloned into a plant transformation vector that also included a herbicide resistance gene (spectinomycin) and was flanked by agrobacterium LB and RB t-DNA sequences (Figure 1 ). The vector was transformed into Agrobacterium tumefasciens (LBA4404 strain) by electroporation, positive colonies were selected and cultured using standard techniques. To demonstrate that this technology would have broad utility in all plant species, this vector was transformed into Arabidopsis thaliana using floral dip method (Clough & Bent, 1998) and stable transgenic lines were generated. | [0135] It should be noted that although the soybean expansin gene promoter was used in this example, other root promoters are known in the art (for example (Y. Li et al., 2019; Marques-Bueno et al., 2016). It would be expected by those of ordinary skill in the art that any root promoter selected from any species would be expected to function equivalently to drive expression in roots. It should also be noted that the technology of the invention would be expected to work if the carbonic anhydrase protein was expressed throughout the plant, or in other plant tissues, so long as the expression domain encompassed expression in roots. | [0136] An experiment was performed to demonstrate that plants expressing secretable/transportable carbonic anhydrase in root cells resulted in carbonic anhydrase activity in the extracellular environment of the root. Here, transformed plants and wild type control plants were grown for six-weeks in hydroponic conditions. At six weeks, individual plants were transferred to 15ml of fresh hydroponic media and allowed to grow for two days. Following this two-day period, the hydroponic solution was sampled and used for carbonic anhydrase activity assays to measure the amount of carbonic anhydrase activity that had been secreted/transported from the roots into the hydroponic medium. | [0137] Here, 10OpI of hydroponic solution was added to a 2ml snap lid microcentrifuge tube containing 1050pl of a 20 mM Tris-HCI solution (pH 8.3) with 0.003% bromothymol blue and 1 OOpI extraction buffer (200mM Tris HCI pH8.3, 1 mM EDTA, 20mM MgCl2, 50mM NaCI, 100mM Na2SO4). Subsequently, 750pl of ice chilled CO2 saturated water (generated by soda stream) was added to start the reaction. The time taken for acolour change from blue (pH 8.3) to yellow (pH 5.3) was recorded and used to calculate enzyme activity as in Example 2. The reaction was performed on ice. | [0138] The carbonic anhydrase activity was significantly increased at 11x higher in the hydroponic medium samples from transgenic plants than from hydroponic medium samples from wild-type control plants (P=0.029404, one-tailed Student’s t-test, unequal variance) (Figure 2B). Thus, plants transformed with the invention successfully expressed and secreted active carbonic anhydrase protein into the extracellular environment of the root, which in turn catalysed conversion of CO2 to bicarbonate. | [0139] Example 3 | [0140] To demonstrate that this technology also works to sequester CO2 in the soil a separate experiment was performed on soil grown plants. Given that carbonic anhydrase catalyses the conversion of CO2 and water into bicarbonate and a proton, the sequestration of atmospheric CO2 in the soil is directly proportional to the pH change of the soil. Here, transgenic plants and wild type plants (described in Example 2) were grown in 6.5cm pots containing 110g Westland John Innes No.3 Mature Plant Compost for six weeks. Soil control pots not containing any plants were also constructed. For each pot, the pH of the soil 2cm below the surface was measured in three random locations using a HANNA™ soil pH tester (HI-981030). As shown in Figure 2C, the soil pH in the pots containing transgenic plants of the invention was significantly lower than either pots containing no plants (‘soil control’) (P=0.000092, one-tailed Student’s t-test, unequal variance), or pots containing wild-type plants (P=0.000449, one-tailed Student’s t-test, unequal variance). Thus, pots containing plants of the invention sequestered more CO2 in the soil than pots containing control plants or pots containing no plants. | [0141] Plants were also imaged as they grew. There were no obvious differences in the phenotype between transgenic and wild type plants across plant development, growth rate, flowering, or seed set (Figure 2F). Thus, secreting carbonic anhydrase from roots, and sequestering CO2 in the soil as bicarbonate, is not deleterious to plant growth.Example 4 | [0142] A CO2 soil flux experiment was conducted to further demonstrate that transgenic plants of the invention increased the rate at which CO2 diffuses from the air into the soil and is converted into bicarbonate. | [0143] Here, transgenic plants and wild type plants (described in Example 2) were grown in 6.5cm pots containing 110g Westland John Innes No.3 Mature Plant Compost for 6 weeks. After 6 weeks all above ground biomass (i.e. leaves, stems etc) was removed and the pot containing all of the below ground biomass in soil was placed in a LI-COR 6800 small plant chamber in complete darkness (achieved by covering chamber in tinfoil). The CO2 that was absorbed or emitted by the soil in the pot was then measured using the LI-COR 6800. To do this, the chamber was equilibrated in CO2 free air for 1 hour. After 1 hour, the CO2 level was raised to 1000 ppm (~2.5x atmospheric CO2 concentration). Following 1 minute of acclimation, the soil CO2 sequestration rate was measured every second for a 30-m inute recording window. Net carbon sequestration was calculated by summing the carbon sequestration over the recording window. As shown in Figure 2D, this revealed that pots containing control plant roots did not sequester CO2 from the air stream, and instead produced CO2 through soil respiration. In contrast, pots containing roots of transgenic plants of the invention depleted CO2 from the air stream. Thus, plants of the invention facilitated CO2 sequestration into the soil. Moreover, the magnitude of this sequestration is substantially larger than the CO2 released through soil respiration. | [0144] Example 5 | [0145] To demonstrate that other carbonic anhydrase genes from other species can be used in different embodiments of this invention we expressed a carbonic anhydrase from the diatom Conticribra weissflogii (also known as Thalassiosira weissflogii) [SEQ ID NO: 2], As above this carbonic anhydrase was translationally fused to the experimentally characterised signal peptide from the carrot (Daucus carota) extensin gene (G. Li et al., 2009) [SEQ ID NO: 3], This fusion protein was placed under the control of a root specific promoter from the soybean expansin gene (Glyma.17G133100) [SEQ ID NO:6], and cloned into a plant transformation vector that also included a herbicide resistance gene (spectinomycin) and was flanked by agrobacterium LB and RB t-DNA sequences. The vector was transformed intoAgrobacterium tumefasciens (LBA4404 strain) by electroporation, positive colonies were selected and cultured using standard techniques. This vector was transformed into Arabidopsis thaliana and stable transgenic lines were generated. | [0146] Seeds of transgenic plants expressing the secretable/transportable carbonic anhydrase from Conticribra weissflogii (SEQ ID NO 2 and 9) and seeds of wild type plants were germinated on >2 Murashige and Skoog + 1 % sucrose + 2.5mM MES agar plates. After 7 days seedlings were transferred to 96 well plates with only the roots entering each well. Each well in the 96 well plate contained 350pl of >2 Murashige and Skoog + 1 % sucrose solution and 30mg L-1 bromocresol purple. After four hours the seedlings were removed and the absorbance at 429 nm was measured using a plate reader. Carbonic anhydrase activity was estimated from the rate of change in pH over the four hour time period. The carbonic anhydrase activity was significantly higher in the root environment of the transgenic plants than in the root environment of the wildtype control plants (P=0.017435, one-tailed Student’s t-test, unequal variance) (Figure 2E). Thus, plants transformed with the secretable/transportable carbonic anhydrase from Conticribra weissflogi successfully expressed and secreted active carbonic anhydrase protein into the extracellular environment of the root, which in turn catalysed conversion of CO2 to bicarbonate. This demonstrates that carbonic anhydrase proteins from any species and any carbonic anhydrase subtype would be by expected to work equivalently. | [0147] Example 6 | [0148] To demonstrate that soybean plants can be engineered such that their roots secrete active carbonic anhydrase proteins into the extracellular environment we translationally fused an experimentally characterised signal peptide from the carrot (Daucus carota) extensin gene provided in Example 2 [SEQ ID NO: 3] with the soybean carbonic anhydrase provided in Example 1 [SEQ ID NO: 1 and SEQ ID NO: 8], This fusion protein was placed under the control of a root specific promoter from the soybean expansin gene (Glyma.17G133100) [SEQ ID NO:6], and cloned into a plant transformation vector that also included a herbicide resistance gene (spectinomycin) and was flanked by agrobacterium LB and RB t-DNA sequences (Figure 1 ). The vector was transformed into Agrobacterium tumefasciens culturedusing standard techniques. This vector was transformed into Glycine max and stable engineered lines were generated. Engineered and azygous control plants were grown for 3-weeks on Levington advance F2S Seed & Modular & Sand Compost before washing roots and transplanted to 4.5L hydroponic boxes. Plants were grown on hydroponic media for two weeks as previously described by Hata & Futamura (2020). After two weeks the hydroponic media was replenished with fresh media and plants were grown for five days depending on the rate of plants consuming hydroponic media. Samples of hydroponic media from hydroponic boxes containing either control or engineered plants were filtered through a Falcon 40pm cell strainer to remove plant debris. Proteins present in the filtered samples were then isolated and concentrated using Pierce 10kD MWCO protein concentrating column. The total protein concentration of each isolated protein sample was calculated using a Bradford Protein assay and total protein concentration adjusted to be equal across all samples. To measure Carbonic anhydrase activity an adapted version of the protocol described in Ozdemir ((2009) was used. Here, 160pl of concentrated hydroponic media samples were added to 120pl of 50mM Tris-HCI pH 7.5 in a well of a 96-well microplate. Following this, 30 I of 10mM p-Nitrophenyl acetate dissolved in acetonitrile was added to each well to start the colorimetric assay. A spectrophotometer plate reader was used to measure absorbance in each well at 400nm over a 16-hour period at 25C. Carbonic anhydrase activity was reported as pM of p-Nitrophenol synthesised per second. Mean carbonic anhydrase activity was calculated from two independent azygous lines and three independent engineered lines (Figure 4A). Protein samples isolated from hydroponic medium that contained azygous plants exhibited a baseline p-nitrophenyl hydrolysis activity. Protein samples isolated from hydroponic medium that contained engineered plants exhibited a significantly higher p-nitrophenyl hydrolysis activity. This is consistent with the presence of secreted carbonic anhydrase in the hydroponic medium that contained engineered plants. | [0149] Plants were also imaged as they grew on soil. There were no obvious differences in the phenotype between engineered soybean plants and control plants across plant development, growth rate, flowering, or seed set (Figure 4F). Thus, secreting carbonic anhydrase from roots, and sequestering CO2 in the soil as bicarbonate, was not deleterious to plant growth.Example 7 | [0150] To demonstrate that soybean plants that have been engineered to secrete active carbonic anhydrase proteins into the extracellular environment enable sequestration of CO2 in the soil the following experiment was performed. Engineered plants expressing a secretable carbonic anhydrase in root hair cells (as described in Example 6) and wild-type control plants were grown in 13cm pots containing 1 :1 :2:2 Levington M3 compost, Melcourt topsoil, Melcourt sharp sand and perlite mixed with 5ml Miracle- Gro All Purpose Continuous Release Plant Food. When plants were 17-weeks old a 2.1 cm diameter soil sampler probe was used to collect a soil core at a random location near the root zone from each pot and transferred to falcon tube. An equal volume to soil weight of ddH2O was added and mixed for 30 minutes and allowed to stand for 1- hour. Using a METLER pH probe the pH of the soil slurry was measured. The pH of the soil from the pots containing engineered plants of the invention was significantly lower (P=0.00798, one-tailed Student’s t-test, unequal variance) than pots containing wild-type plants (Figure 4B). This reduction in soil pH is consistent with the presence of active carbonic anhydrase protein, and thus an increased concentration of bicarbonate, in the soil of pots containing engineered plants of the invention. Thus, soil in which plants of the invention were grown sequestered more CO2 than soil in which control plants were grown. | [0151] Example 8 | [0152] To demonstrate that carbonic anhydrase genes from any species can be used in engineered plants of the invention the soybean carbonic anhydrase gene used in Example 1 and Example 2 above was exchanged for a carbonic anhydrase gene from a marine alga [SEQ ID NO: 2], All other components of the vector for plant transformation were kept the same. To demonstrate that the carbonic anhydrase protein that is expressed is secreted from soybean roots and is active engineered plants of the invention and azygous control plants were grown for 3-weeks on Levington advance F2S Seed & Modular & Sand Compost before washing roots and transplanting to 4.5L hydroponic boxes. Plants were supported on hydroponic media as previously described by (Hata & Futamura 2020). Plants were grown hydroponically for 1-week. Hydroponic media was then replenished with fresh media and plants weregrown for a further 7-days. Samples of media from hydroponic boxes containing only control or engineered plants was isolated and filtered through a Falcon 40pm cell strainer to remove plant debris. The proteins present in the filtered samples were then isolated and concentrated using Pierce 10kDMWCO protein concentrating column. The total protein concentration of each sample was calculated using a Bradford Protein assay and enzyme activity was normalised to total protein content. To measure Carbonic anhydrase activity an adapted version of protocol described in Ozdemir (2009). was used. Here, 160 I of concentrated hydroponic media samples were added to 120pl of 50mM Tris-HCI pH 7.5 in a well of a 96-well microplate. Following this, 30pl of 10mM p-Nitrophenyl acetate dissolved in acetonitrile was added to each well to start the colorimetric assay. A spectrophotometer plate reader was used to measure absorbance in each well at 400nm over a 11 -hour period at 25C. | [0153] As shown in Figure 4C, protein samples isolated from hydroponic medium that in which azygous plants were grown exhibited a baseline p-nitrophenyl hydrolysis activity. Protein samples isolated from hydroponic medium that in which engineered plants of the invention were grown exhibited a significantly higher p-nitrophenyl hydrolysis activity. This is consistent with the presence of secreted carbonic anhydrase in the hydroponic medium that contained engineered plants. | [0154] Example 9 | [0155] To demonstrate that soybean plants that have been engineered to express active carbonic anhydrase proteins on the surface of their roots to enable sequestration of CO2 in the soil, the following experiment was performed. As above engineered soybean plants where soybean carbonic anhydrase [SEQ ID NO: 3] was translationally fused with experimentally characterised signal peptide and transmembrane domain from pea (Pisum sativum) [SEQ ID NO: 4 and SEQ ID NO:5], This fusion protein was placed under the control of a root specific promoter from the soybean expansin gene (Glyma.17G133100) [SEQ ID NO:6], and cloned into a plant transformation vector that also included a herbicide resistance gene (spectinomycin) and was flanked by agrobacterium LB and RB t-DNA sequences (Figure 1 ). The vector was transformed into Agrobacterium tumefasciens cultured using standard techniques. This vector was transformed into Glycine max and stable engineered lines were generate. Engineeredand azygous control plants were grown in 13cm pots containing John Innes Cereal Mix. When plants were 13-weeks old a 2.1 cm diameter soil sampler probe was used to collect a soil core sample at a random location near the root zone from each pot and transferred to falcon tube. An equal volume to soil weight of ddH2O was added and mixed for 30 minutes and allowed to stand for 1 -hour. The pH of the soil slurry was measured using a METLER pH probe. As shown in Figure 4D, the pH of the soil in the pots in which engineered plants of the invention were grown was significantly lower than the pH of the soil in the pots containing wild-type plants. This reduction in soil pH is consistent with the presence of active carbonic anhydrase protein, and thus an increased concentration of bicarbonate, in the soil of pots containing engineered plants of the invention. Thus, pots containing engineered plants of the invention sequestered more CO2 in the soil than pots containing control plants or pots containing no plants. | [0156] Example 10 | [0157] To demonstrate that other carbonic anhydrase genes from other species can be engineered and localised extracellularly on root hairs of soybean roots engineered plants used in Figure 4C and their respective azygous control plants were grown for 3-weeks on Levington advance F2S Seed & Modular & Sand Compost and transplanted to 4.5L hydroponic boxes. Plants were supported on hydroponic media as previously mentioned by Hata & Futamura (2020). Plants were grown hydroponically for 2-weeks with media refreshed weekly. To measure carbonic anhydrase activity on root surface an adapted carbonic anhydrase p-nitrophenyl hydrolysis activity protocol taken from Ozdemir (2009) was used. 500mg fresh weight of soybean roots were removed were briefly washed with sterile water to remove excess hydroponic media and then placed in 30ml beaker containing 18ml 50mM Tris- HCI pH 7.5. 2ml 10mM p-Nitrophenyl acetate dissolved in acetonitrile was used to start the reaction. Absorbance of 300pl samples at 400nm was recorded at 1 -minute and 33 minutes using spectrophotometer plate reader. Carbonic anhydrase activity was reported as pM of p-Nitrophenol synthesised per second. | [0158] Engineered plant roots demonstrated significantly higher (P=0.030458, one-tailed Student’s t-test, unequal variance) p-nitrophenyl hydrolysis activity compared tocontrol plant roots (Figure 4E). This is consistent with the detection of carbonic anhydrase activity extracellularly from roots of engineered plants. | [0159] Example 11 | [0160] To demonstrate that carbonic anhydrase enzymes can be engineered to be localised extracellularly on the plasma-membrane of the cell, a reporter-gene fusion was made and tested in protoplasts. Here, Conticribra weissflogii carbonic anhydrase [SEQ ID NO: 2] was translationally fused with the coding sequence for a fluorescent protein to produce a gene-reporter fusion. This gene-reporter fusion was then translationally fused at the N-terminus and C-terminus with a signal peptide and transmembrane domain, respectively, from the pea (Pisum sativum) gene PsBP80 [SEQ ID NO: 4 and SEQ ID NO:5], This final fusion protein was placed under the control of a cassava vein mosaic virus promoter (Verdaguer et al. (1996)) and cloned into a plant transformation vector. To provide a cytoplasmic localised control, the Conticribra weissflogii carbonic anhydrase translationally fused with the coding sequence for a fluorescent protein, without the PsPB80 signal peptide and transmembrane domain, was also placed under the control of a cassava vein mosaic virus promoter (Verdaguer et al. (1996)) and cloned into a plant transformation vector. | [0161] Soybean protoplasts were transfected with these two expression vectors following the protocol by Sultana et al. (2019). After 2-days, the transfected protoplasts were imaged using a Leica TCS SP5 confocal microscope. Protoplasts expressing Conticribra weissflogii carbonic anhydrase fused to the coding sequence for a fluorescent protein, without the PsPB80 signal peptide and transmembrane domain, showed a clear cytosolic localisation (Figure 5A). In contrast, protoplasts expressing Conticribra weissflogii carbonic anhydrase fused to the coding sequence for a fluorescent protein with the PsBP80 signal peptide at the N-terminus and the PsBP80 transmembrane domain at the C-terminus localised to the plasma membrane (Figure 5B).Example 12 | [0162] To demonstrate that promoters used for generation of engineered plants herein drive expression in specific root tissues, GUS reporter lines were generated. Here, pGmEXPA7 (SEQ ID NO:6) and pGmPIN2b (SEQ ID NO:7) were each used independently to drive expression of GUS(Cat1 +) (beta-glucuronidase gene with castor bean catalase first intron Cat1 ) . These promoter-GUS fusions were separately cloned into a plant transformation vector that included a herbicide resistance gene (Kanamycin) and was flanked by agrobacterium LB and RB t-DNA sequences. The resulting vectors were transformed into Agrobacterium tumefasciens (LBA4404 strain) by electroporation and positive colonies were selected and cultured using standard techniques. These agrobacterium strains were used to transform Arabidopsis thaliana via the floral dip method (Clough & Bent, 1998). Engineered plants were germinated on >2 Murashige and Skoog + 1 % sucrose + 2.5mM MES agar plates. After 10 days, seedlings were transferred to 6-well plates and GUS histochemical staining was performed. 5ml of GUS staining buffer (0.5mM KsFe(CN)6, 0.5mM K4Fe(CN)e 3H2O, 50mM Sodium Phosphate buffer, 10mM Na2EDTA H2O, 1 mM X-Gluc and 0.1 % Triton- X (v:v)) was added to seedlings and incubated at 37C for 3-hours. Seedlings were washed and cleared with 70% ethanol overnight. Stained and chlorophyll cleared seedlings roots were imaged using an Optika B-383FL microscope combined with OneView camera and imaging software. | [0163] GUS expression driven by the pGmPIN2b promoter [SEQ ID NO:6) was localised to the epidermis of root tip and some expression extending up the primary root (Figure 5C). GUS expression driven by the pGmEXPA7 promoter was localised to the root hair cells (Figure 5D). | [0164] Example 13 | [0165] To demonstrate that engineered plants of the invention enable increased accumulation of soil inorganic carbon the following experiment was performed. Engineered plants described in Example 6 that express a secreted soybean carbonic anhydrase from root hair cells [SEQ ID NO: 6] and azygous control plants were grown in 13cm pots containing 1 :1 :2:2 Levington M3 compost, Melcourt topsoil, Melcourt sharp sand and perlite soil mixed with 5ml Miracle-Gro All Purpose Continuous Release Plant Fooduntil the end-of-life cycle. When seeds were harvested, and soil was dry, the dried biomass and roots in the soil were removed and the remaining soil was sieved through 2mm sieve. The soil samples were sent to Eurofins AgroTesting UK for soil Carbon Check to analyse soil inorganic (SIC) and organic carbon (SOC) content. | [0166] Mean inorganic carbon content of soil from pots in which engineered plants were grown was higher than soil from pots in which azygous control plants or no plants were grown (Figure 6A). | [0167] Example 14 | [0168] To demonstrate that exogenous soil treatments can be used in combination with engineered plants of the invention to enhance CO2 sequestration in the soil the following experiment was performed. Here, engineered Arabidopsis thaliana plants described in Example 2 expressing a secretable carbonic anhydrase in root hair cells and wild-type control plants were grown in 6.5cm pots containing 160g of Levington advance F2S Seed & Modular & Sand Compost mixed with 4.16g L-1 Ca(OH)2. The pH of the soil was adjusted to pH 8 to facilitate enhanced conversion of HCO3- to CO3- which can then combine with Ca from Ca(OH)2 to form CaCOs. | [0169] Plants were grown for 10-weeks. At 10 weeks, all above soil biomass was removed and the soil was sent to Eurofins AgroTesting UK for soil Carbon Check to analyse soil inorganic (SIC) and organic carbon (SOC) content. Soil in which engineered plants of the invention were grown exhibited increased soil inorganic carbon (Figure 6B) and significantly higher soil inorganic carbon normalised against soil organic carbon (P=0.002078, one-tailed Student’s t-test, unequal variance) (Figure 6C). This is consistent with the presence of carbonic anhydrase activity, and thus enhanced conversion of CO2 to bicarbonate, in the soil in which engineered plants of the invention were grown. Thus, soil treatments can be used in conjunction with engineered plants of the invention to enhance CO2 sequestration. It would be expected by those of ordinary skill in the art that any soil treatment rich in positively charge cations such as magnesium oxide or cations derived from crushed rock soil treatments or fertilizer treatments or deploying the technology on soils that are naturally richer in cations would be expected to function equivalently when used with our invention to increase inorganic soil carbon, our invention to increase inorganic soil carbon.Example 15 | [0170] To demonstrate that engineered plants of the invention enable increased accumulation of soil inorganic carbon the following experiment was performed. Engineered soybean plants described in Example 8 expressing soybean carbonic anhydrase that is anchored to the plasma membrane of root hair cells and their respective azygous control plants were grown in 13cm pots containing 1 :1 :2:2 Levington M3 compost, Melcourt topsoil, Melcourt sharp sand and perlite soil mixed with 5ml Miracle-Gro All Purpose Continuous Release Plant Food until the end-of-life cycle. When seeds were harvested, and soil was dry, the dried biomass and roots in the soil were removed and the remaining soil was sieved through 2mm sieve. The soil samples were sent to Eurofins AgroTesting UK for soil Carbon Check to analyse soil inorganic (SIC) and organic carbon (SOC) content. | [0171] Soil in which engineered plants of the invention were grown exhibited significantly increased soil inorganic carbon (P=0.032395, one-tailed Student’s t-test, unequal variance) (Figure 6D) and significantly higher soil inorganic carbon normalised against soil organic carbon (P=0.048304, one-tailed Student’s t-test, unequal variance) (Figure 6E) than soil in which control plants were grown. | [0172] This is consistent with the presence of increased carbonic anhydrase activity, and thus enhanced conversion of CO2 to bicarbonate to generate inorganic carbon in the soil in which plants of the invention were grown. Thus demonstrating engineered plants of the invention to enhance carbon sequestration in the soil. | [0173] REFERENCES | [0174] Boone, C. D., Gill, S., Habibzadegan, A., & McKenna, R. (2013). 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(WO2024/149976)|[0001] CARBON SEQUESTRATION WITH TRANSGENIC PLANTS EXPRESSING CARBONIC ANHYDRASE | [0002] FIELD OF THE INVENTION | [0003] The present invention relates to the field of biotechnology, and more specifically to compositions and methods for enhancing sequestration of atmospheric CO2 in soils using plants. Genetically modified plants expressing enzymes to facilitate CO2 sequestration are provided, along with enzyme sequences and their use in various applications. The invention further concerns parts of such modified plants, such as plant cells, plant parts, plant organs, fruits, seeds, embryos, germplasm and processed plant products. | [0004] BACKGROUND | [0005] Anthropogenic greenhouse gas emissions have already caused an approximately 1 °C rise in global surface temperature over pre-industrial levels (Masson-Delmotte, 2018). Carbon dioxide (CO2) emissions have been the main contributor to this warming and efforts to meet the requirements of the Paris agreement to stay below 2°C, and ideally 1.5°C, to mitigate against the worst effects of climate change (Horowitz, 2016) will require the combined effort of reducing global CO2 emissions and the development of technologies that increase the sequestration of atmospheric CO2 (Masson-Delmotte, 2018). | [0006] SUMMARY OF INVENTION | [0007] The inventors have unexpectedly found that carbonic anhydrase genes expressed in root cells can enable CO2 sequestration, for example as bicarbonate, in the extracellular environment of the roots. In doing so, they have provided a solution to sequestration of atmospheric CO2 that is relevant for industrial biotechnology. Prior to the present invention, carbonic anhydrase genes have not been over-expressed in plant root cells, nor have carbonic anhydrase proteins been exported from plant root cells, nor have carbonic anhydrase proteins been over-expressed on the surface of plant root cells or in the extracellular environment. Thus, the approach used herein isnovel. Overall, the present invention achieves enhanced carbon sequestration from the atmosphere with no observable negative or deleterious anatomical, physiological, biochemical or developmental effects on modified plants. | [0008] The present invention provides a plant which comprises, or whose heritable genetic material comprises, a gene encoding a secretable/transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is secreted/transported from the roots of the plant into the extracellular environment. Therefore, the invention provides a plant in which the genetic material has been modified, the modification being such that the modified plants express carbonic anhydrase or a portion thereof, in at least some root cells of the plant. This expression in root cells is additional to any endogenous expression of carbonic anhydrase in the plant, in particular in the plant root where endogenous expression does not provide secretable/transportable carbonic anhydrase or any substantial carbonic anhydrase enzymatic activity in the extracellular environment of the plant root. | [0009] The expressed carbonic anhydrase may lead to increased levels of extracellular root carbonic anhydrase enzymatic activity, or in other words carbonic anhydrase enzymatic activity in the extracellular environment of the roots of the plant. The extracellular root environment may, for example, be the soil or any other location where a plant may germinate or grow or be cultivated including aeroponic and/or hydroponic growth environments. | [0010] Also provided herein is a plant wherein the carbonic anhydrase is over-expressed in the extracellular environment of the root cells in comparison to a plant which does not comprise, or whose heritable genetic material does not comprise, a gene encoding a secretable/transportable carbonic anhydrase protein under the control of a promoter active in root cells. | [0011] In addition or alternatively, provided herein is a plant wherein the heritable genetic material of the plant has been modified to contain a gene encoding a secretable/transportable carbonic anhydrase protein under the control of a promoter active in root cells. The genetic modification results in a carbonic anhydrase that isover-expressed in the extracellular environment of the plant root in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells or has not been altered. | [0012] In some embodiments, the gene encoding the secretable/transportable carbonic anhydrase protein further comprises a signal peptide sequence for directing secretion/transport of the carbonic anhydrase into the extracellular environment of the plant root. | [0013] Also provided herein is a polynucleotide sequence comprising a sequence coding for a polypeptide sequence under the control of a suitable promoter, wherein the polypeptide sequence comprises a carbonic anhydrase sequence and a signal peptide sequence, wherein the promoter is active in plant roots and capable of driving expression of the carbonic anhydrase in root cells, wherein the signal peptide sequence is capable of directing secretion/transport of the carbonic anhydrase into the extracellular environment of a plant root. The signal peptide sequence of any polynucleotide sequence disclosed herein may either be natively encoded or translationally fused to the carbonic anhydrase sequence to ensure secretion/transport of the carbonic anhydrase to the extracellular environment of the plant root. The signal peptide sequence for directing secretion/transport may be derived from any secreted protein that is transported to the extracellular environment by a protein secretion pathway. The signal peptide sequence may also be derived from the extensin protein, and in some embodiments it may be derived from a carrot plant or derived from the vacuolar sorting protein, or derived from a pea plant. | [0014] The carbonic anhydrase (including the polynucleotide encoding it or the peptide itself) is transportable and, in some embodiments, may be secreted or secretable. Additionally, in some embodiments the carbonic anhydrase may be attached to the outside of the cell or to the plasma membrane by a transmembrane domain, or a transmembrane helix, or a membrane anchor, or a glycosylphosphatidylinositol (GPI) anchor, or any other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell.The promoter, signal peptide sequence, or carbonic anhydrase of the polynucleotide or plant disclosed herein may be derived from a gene from the same plant species or variety as the plant in which it is expressed. The promoter may be root-specific, and in some embodiments it may be root hair and/or root epidermis specific. The expression domain of the promoter may also include other cells and tissues of the plant so long as the expression domain includes the root. | [0015] Also provided herein are carbonic anhydrases further comprising a transmembrane domain or a membrane anchor sequence. The carbonic anhydrase may be an a, (3, y, 5, q, 0, or i subtype carbonic anhydrase. In some embodiments it is a monomer. | [0016] Provided herein are polypeptide sequences encoded by the polynucleotide disclosed herein. A plant cell, cell line or progeny thereof comprising the polynucleotide sequence or polypeptide sequence disclosed herein are also provided. The progeny may be a progeny of the plant cell or a progeny of the cell line. | [0017] In some embodiments, the plant, polynucleotide, polypeptide, cell, cell line or progeny disclosed herein may derive from a plant wherein the plant is a crop. In some embodiments the plant is a row or cover crop. In some embodiments, the plant is selected from a corn, soybean, pea, cotton, canola, camelina, potato, tomato, sugar beet, cassava, sweet potato, alfalfa, wheat, barley, sorghum, oat, sorghum, millet, rye, teff, rice, or clover, cress, brassicas, vetch and prairie grasses. Additionally, the polynucleotide, polypeptide, cell, cell line or progeny disclosed herein may derive from a plant wherein the plant is a tree. In some embodiments wherein the tree is poplar, spruce, pine, eucalyptus, oil palm or rubber. | [0018] Also provided herein is the plant, polypeptide, polynucleotide, cell, cell line or progeny disclosed herein, where more carbon is sequestered into the extracellular environment of the plant in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells.Additionally provided is a plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus, cell culture, pollen grain or seed, derived or obtained from the plant disclosed herein. | [0019] Provided herein is a vector comprising the polynucleotide sequence disclosed herein. The vector is optionally a plasmid. Plasmids in accordance with the invention may further comprise one or more other elements selected from: an enhancer, a plant selectable marker, a multicloning site, or a recombination site. The structure, modification, propagation and generation of vectors or plasmids is well known to a person of ordinary skill in the art. | [0020] Also provided are compositions for transformation of plant cells comprising the polynucleotide, vector, or plasmid disclosed herein, optionally comprising microparticles coated with said polynucleotide or said vector. The microparticles may be of metal or synthetic material. In some embodiments the metal is tungsten or gold. | [0021] Also provided is a bacterium comprising the polynucleotide, plasmid, or vector disclosed herein, optionally wherein the bacterium is E coli. or Agrobacterium sp. In some embodiments the agrobacterium is A. tumefaciens. | [0022] Also provided herein are plants comprising the polynucleotide disclosed herein stably integrated into the genome thereof; and in some embodiments heritably integrated into the genome thereof. | [0023] Provided herein are methods of producing a plant or seed, comprising the steps of:- | [0024] (a) providing the vector or plasmid disclosed herein; | [0025] (b) activating the promoter operably linked to the polypeptide coding DNA;| [0026] (c) optionally wherein the polypeptide is overexpressed in the extracellular environment of the cell in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells.Methods for increasing the capacity of a plant to sequester carbon in the soil are also provided herein, the methods comprising altering the heritable genetic material of the plant such that a carbonic anhydrase protein is transported from the roots of the plant into the extracellular environment. The altering of heritable genetic material may comprise inserting at least one polynucleotide into the heritable genetic material of a plant cell. The altering of heritable genetic material may also comprise genetically editing the heritable genetic material of a plant cell. | [0027] A method in accordance with the invention may employ classical and well-known techniques of genetic modification, involving a method of transformation, whereby the polynucleotide of the invention is incorporated into a plant genome. Any necessary root cell expression regulatory elements may be present. In some embodiments this incorporation is stable and heritable so as to permit introduction of the modification into particular lines of crop plants; advantageously for the purposes of crop improvement or breeding programmes. A gene editing method may be used to incorporate or give rise to the polynucleotide of the invention. | [0028] Although various methods for gene editing are known, including TALE Nucleases (TALENs) or Zinc Fingers, a CRISPR system may also be used. For example a CRISPR-Cas system may be used whereby a guide RNA (gRNA) is selected to target the action of a CRISPR-Cas protein to a desired genomic locus resulting in a homologous recombination (HR) event or non-homologous end joining repair, i.e. insertion-deletion of the polynucleotide into the plant genome. | [0029] Therefore, the polynucleotide disclosed herein may include a polynucleotide encoding a CRISPR-Cas protein, optionally also a guide RNA (gRNA), wherein the gRNA directs the CRISPR-Cas protein to the locus of an endogenous carbonic anhydrase coding sequence in the plant cell genome, optionally wherein a regulatory element is inserted so as to cause expression of the carbonic anhydrase in at least some root cells of the plant. | [0030] Also provided herein are processed plant products obtained from the plant or the plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus culture, pollen grain or seed disclosed herein; optionally wherein the processed product comprises adetectable nucleic acid sequence of (i) a transportable carbonic anhydrase downstream of a gene expression regulatory element active in at least some of the root cells of a plant, or (ii) a polynucleotide or at least a portion of a polynucleotide disclosed herein. | [0031] BRIEF DESCRIPTION OF THE FIGURES | [0032] The invention will be further described by way of reference to the examples and accompanying figures. | [0033] Figure 1 depicts an illustrative diagram of the genetic vector used for soybean transformation to express a secreted-version of a soybean carbonic anhydrase in roots. | [0034] Figure 2 demonstrates that the carbonic anhydrase activity of the extracellular environment around the roots is enhanced in genetically engineered plants compared to wild type (control plants). A) shows carbonic anhydrase activity in a supernatant following enzyme liberation from root tissue of control and engineered soybean hairy roots. Standard error bars shown. B) shows carbonic anhydrase activity in the hydroponic solution in which control and genetically engineered plants were grown. Standard error bars shown. C) shows that genetically engineered plants produce a measurable decrease in soil pH relative to both soil-only control pots and control plants. This demonstrates that carbonic anhydrase has catalysed the conversion of CO2 in the air into bicarbonate and a proton in the soil. Standard error bars shown. D) shows that engineered plant roots sequester CO2 from the atmosphere, which control plant roots are not able to do. CO2 sequestration is shown for pots containing soil and plant roots (above ground tissue excised) over a 30-m inute measurement period. Standard error bars are shown. E) shows carbonic anhydrase activity in the extracellular environment of the roots of wild type and transgenic plants. This shows that transgenic plants have higher carbonic anhydrase activity. F) shows that there are no discernible differences in growth phenotype between control and genetically engineered Arabidopsis plants that secrete carbonic anhydrase from roots. Photo taken of 5-week-old control plant (left) and engineered plant of this invention (right). Scale bar represents 5cm.Figure 3 depicts a general schematic for the DNA sequence of the fusion carbonic anhydrase protein. Such constructs are typified by the inclusion of a genetic sequence encoding a protein with carbonic anhydrase activity, a promoter ensuring the sequence is expressed e.g. in plant root tissues, a terminator, and a peptide sequence designating cellular export e.g. an N-terminus signal peptide. | [0035] Figure 4 demonstrates that the carbonic anhydrase activity of the extracellular environment around the roots is enhanced in genetically engineered plants compared to wild type (control plants). A) shows that carbonic anhydrase activity in the hydroponic solution in which genetically engineered soybean plants that transport carbonic anhydrase from the roots of the plant into the extracellular environment were grown is higher relative to control plants. Standard error bars shown. B) shows that genetically engineered soybean plants that transport carbonic anhydrase from the roots of the plant into the extracellular environment produce a measurable decrease in soil pH relative to control plants. This demonstrates that carbonic anhydrase has catalysed the conversion of CO2 in the air into bicarbonate and a proton in the soil. Standard error bars shown. C) shows that genetically engineered soybean plants with carbonic anhydrase embedded on root surface produce a measurable decrease in soil pH relative to control plants. This demonstrates that carbonic anhydrase has catalysed the conversion of CO2 in the air into bicarbonate and a proton in the soil. Standard error bars shown. D) shows increased carbonic anhydrase activity in the hydroponic solution in which genetically engineered soybean plants with an alternative carbonic anhydrase were grown, relative to hydroponic solution in which control plants were grown. Standard error bars shown. E) demonstrates increased carbonic anhydrase activity from the roots of genetically engineered soybean plants relative to control plants. Standard error bars shown. F) shows that there are no discernible differences in growth phenotype between control and genetically engineered soybean plants that secrete carbonic anhydrase from roots. Photo taken of 5-week-old control plant (left) and engineered plant of this invention (right). Scale bar represents 5cm. | [0036] Figure 5 A+B: Confocal images of soybean protoplasts expressing fluorescent protein tagged carbonic anhydrase protein. A) Conticribra weissflogii carbonic anhydrase fused with a fluorescent protein. B) Conticribra weissflogii carbonic anhydrase fused with a fluorescent protein with the PsBP80 signal peptide at the N-terminus of thefusion protein and the PsBP80 transmembrane domain at the C-terminus of the fusion protein. C+D: Light microscope images of GUS stained Arabidopsis thaliana roots. C) GUS staining of Arabidopsis roots expressing GUS under the control of the pGmPIN2b promoter. D) GUS stain of Arabidopsis roots expressing GUS under the control of the pGmEXPA7 promoter. Scale bar represents: A) 10 pm, B) 20 pm, C) 50 pm, D) 50 pm. Arrows on A) highlight cytoplasmic GFP expression and B) highlight fluorescent protein expression localised to plasma membrane of the soybean protoplast. Arrows on C) left image and right image and D) left image, highlight areas of GUS stained root. | [0037] Figure 6 demonstrates carbonic anhydrase activity of the extracellular environment around the roots in genetically engineered plants enhanced inorganic carbon sequestration in soil compared to wild type (control plants) A) Analysis of soil inorganic carbon content demonstrating that the soil in which engineered soybean plants of this invention are grown accumulates more inorganic carbon compared to soil in which control soybean plants are grown and no plants are grown. B) shows that following treatment with hydrated lime Ca(OH)2, soil in which engineered Arabidopsis thaliana plants of the invention are grown accumulates more soil inorganic carbon than soil in which control Arabidopsis thaliana plants are grown. C) shows that the result shown in B is consistent when soil inorganic carbon content is normalised by soil organic carbon content. D) shows that soil in which engineered soybean plants of this invention are grown accumulates more soil inorganic carbon than soil in which control soybean plants are grown. E) shows that the result shown in D is consistent when soil inorganic carbon content is normalised by soil organic carbon content. | [0038] DETAILED DESCRIPTION | [0039] Weathering mediated CO2 sequestration | [0040] One way that CO2 is naturally sequestered from the atmosphere is through the process of chemical rock weathering. This occurs when atmospheric CO2 dissolves in rainwater to form carbonic acid (H2CO3). When carbonic acid encounters carbonate and/or silicate rock a chemical reaction occurs that causes the rock to breakdown and ions of bicarbonate (HCO3 ) and calcium (Ca2+) to be released. These ions are carriedby surface waters to the ocean where they precipitate out and fall to the ocean floor for long-term burial (i.e. hundreds of thousands of years). The ability of this process to facilitate long-term sequestration of atmospheric CO2 has led to the proposal of methods that accelerate the chemical rock weathering. These methods, known as enhanced weathering, involve substantially increasing the surface area of rock exposed to rain (containing dissolved CO2) by mechanically crushing it into dust and spreading it over terrestrial ecosystems. This has been proposed to greatly increases the rate at which rock is weathered, and thus the rate at which CO2 is sequestered from the atmosphere (Strefler et al., 2018). | [0041] Carbonic anhydrase | [0042] Carbonic anhydrases are a group of naturally occurring enzymes that catalyse the interconversion of gaseous carbon dioxide (CO2) and water (H2O) into ions of bicarbonate (HCO3 ) and hydrogen (H+) [CO2 + H2O HCOs” + H+], Carbonic anhydrase is a widely distributed enzyme, with members of this enzyme family found in organisms from across the tree of life, from bacteria and archaea to plants and animals. Given the activity of the enzyme there has been interest in using carbonic anhydrase enzymes in industrial settings to capture CO2 from industrial flue gas (as discussed in Boone et al., 2013 and Steger et al., 2022). WO 2015183935A2 also describes the use of modified carbonic anhydrases to catalyse the removal of CO2 from industrial flue gas. Also disclosed is the use of modified carbonic anhydrases which are affixed to a matrix and cross-linked with mineral ions so that a bicarbonate salt is precipitated out, thereby removing the CO2. This process is used in desalination and extracorporeal CO2 removal. Similarly, WO2013159228A1 describes an industrial process whereby CO2 is contacted with a carbonic anhydrase solution containing an additional absorption compound which together sequester the CO2. | [0043] Carbonic anhydrases (CAs) are metalloenzymes that contain a metal co-factor (typically Zn2+ but in some cases Cd2+, Co2+, Fe2+ and Mn2+ although one newly described class of carbonic anhydrase has been shown to exhibit activity under metal- free conditions (Hirakawa et al., 2021 )). To date, eight classes of carbonic anhydrases have been identified (a, (3, y, 5, q, 9, and i) with varying distribution across the three domains of life, a, (3, and y carbonic anhydrases are present in eukaryotes andprokaryotes, while other classes are found in some species of microalgae and protists. A recently described i-CA has been identified in the microalgae Thalassiosira pseudonana and the gram-negative bacterium Burkholderia territorii. Depending on the class, carbonic anhydrases may be active as monomers, dimers, trimers, tetramers, or octomers. In addition to their diversity in form, carbonic anhydrases have diverse functions between and within organisms. In plants, for example, carbonic anhydrases are present in several different plants tissues and vary in their subcellular localisation (DiMario et al., 2017). All carbonic anhydrases, irrespective of their class or the organism in which they are found, catalyse the same biochemical reaction, i.e. the interconversion of gaseous CO2 and water (H2O) into ions of bicarbonate (HCO3 ) and hydrogen ions (H+) as described above. | [0044] Recently, Matt et al. 2022 have described the expression of a glycosylphosphatidylinositol-anchored membrane-bound extracellular carbonic anhydrase in the calcifying primary mesenchyme cells of sea urchin larva. Extracellular CO2 hydration is demonstrated in these findings to suggest the resulting bicarbonate is taken up by the cell for the construction of carbonate structures that form the skeletal tissue of this organism. | [0045] Plants present an interesting opportunity for harnessing carbonic anhydrase for CO2 sequestration as bicarbonate in the soil and for the long-term sequestration of that bicarbonate via ground waters in an analogous manner to the chemical weathering process. Plant roots are in direct contact with the soil and with gaseous CO2 in the soil, which is itself in equilibrium with atmospheric CO2. | [0046] Historically, plants have been genetically engineered to express and secrete enzymes. Li et al. 2009 describes soybean plants which have been transformed with a construct containing a gene encoding a phytase from the fungus Aspergillus ficuum fused at the N-terminus with a signal peptide sequence from a carrot extensin gene. This recombinant gene was then fused to a promoter from the Arabidopsis Pky10 gene which conferred gene expression in the roots of the transgenic soybean plants. | [0047] Here we propose engineering plants to express in their root cells (specifically the outer cell layer, i.e. epidermal cells) an engineered form of carbonic anhydrase which issecreted from the cell into the extracellular environment. In particular, targeting plants which cover a large surface area of the globe (e.g., crop plant species) would provide a means by which atmospheric CO2 could be sequestered at large scale as bicarbonate ions in the soil. Following transport by surface waters, some of this bicarbonate is expected to be carried to, and buried in, the oceans. | [0048] Bioremediation denotes any process which employs a biological system (such as plants or bacteria) to remove environmental pollutants such as CO2 from natural or industrial settings. Bioremediation methods, such as that presented by the present invention, have particular advantages. Bioremediation often requires fewer resources and less energy than industrial man-made technologies and can be specifically altered through genetic engineering to address the specific needs of a particular environment. Additionally, these biological methods do not produce hazardous waste as byproducts, and therefore do not require expensive specialist waste disposal. | [0049] A need exists in the art to find ways to accelerate long-term CO2 sequestration by utilising bioremediation methods. Moreover, there is a need to achieve this through scalable methods that can be implemented rapidly and globally to urgently address the issue of anthropogenic CO2 release and elevated atmospheric CO2 concentration. The present invention addresses this need by demonstrating that expression of carbonic anhydrase in roots of plants, leading to increased levels of extracellular carbonic anhydrase enzymatic activity, results in enhanced CO2 sequestration through conversion of CO2 to bicarbonate. The present invention also demonstrates that multiple different natural or engineered carbonic anhydrase genes from different species can provide this function in plants. Unexpectedly, the inventors have found that this function can be provided when carbonic anhydrase proteins are secreted from plants, and/or when carbonic anhydrase proteins are anchored to the external periphery of the cell, either through for example a transmembrane domain or an anchor. Optionally, the N-terminus or C-terminus may be fused to a transmembrane domain, transmembrane helix, or a glycosylphosphatidylinositol (GPI) anchor, or other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. The present invention also demonstrates that carbonic anhydrase proteins in various compositional formsdescribed above can be expressed in plants using a variety of promoters that achieve the desired expression in root tissue. | [0050] The following detailed description conveys exemplary embodiments of the present invention in sufficient detail to enable those of ordinary skill in the art to practice the present invention. Features, or limitations of the various embodiments described do not necessarily limit other embodiments of the present invention, or the present invention as a whole. Hence the following detailed description does not limit the scope of the present invention, which is defined only by the claims. | [0051] Conventional techniques in botany, microbiology, tissue culture, molecular biology, chemistry, biochemistry and recombinant DNA technology and bioinformatics for use in employing the present invention are all readily known and available to a person of average skill in the art. Specific techniques are explained fully in the literature. | [0052] In the present specification the term “genetically engineered' is used and as will be familiar to a person of skill in the art this term may encompass the terms “genetically modified” and “gene editing”, each of which is appreciated in the art as having respectively differing meanings and underlying technical methodology. However, the term “modified” in an unqualified sense herein, may be understood more simply to mean “changed”, “altered” or “different”. The terms “altered”, “changed” and “modified” may be used interchangeably herein. The terms "increase", "improve" or "enhance" are used interchangeably herein. | [0053] The present invention provides a plant whose heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment. | [0054] The plant of the invention may be a genetically modified plant, a genetically enhanced plant, a non-naturally occurring plant and/or a genetically engineered plant. In some instances, the plant may be transgenic plant. | [0055] Plants in accordance with the invention may be monocots or dicots; in some embodiments they are crop plants, e.g. fruits, vegetables, cereals, oilseed, andlegumes, and may commonly be used for food, animal feed, biofuel or biomass production. A crop plant is any plant which is grown on a commercial scale for human or animal consumption or use. The plants may also be trees, particularly those popular in forestry and land management, carbon capture and biofuel or biomass production. The plants may be horticultural plants. In some embodiments, the plants are cover crops which are plants used to cover exposed soil between harvesting. Cover crops are utilised to mitigate soil erosion, increase soil fertility and quality, in the conservation of water, management of weeds/pests and diseases and to maintain biodiversity and wildlife in an agroecosystem. Cover crops may be utilized during a fallow period in arable farming. During a fallow period, arable land is not sown with harvestable seed for at least one or more vegetative cycles. This allows the arable land to recover. Cover crops may be sown during a fallow period to assist in the recovery of the land. | [0056] Heritable genetic material denotes any polynucleotide sequence and any associated genetic elements in any cell or organelle which is capable of being passed from one generation to a subsequent generation through sexual or asexual reproduction. Sexual plant breeding methods may include propagation. Asexual reproduction, also known as clonal propagation, by way of grafting plant cuttings is also considered as the incorporation of heritable genetic material into the genome of the plant. The heritable genetic material may therefore only be present in part of the plant. | [0057] The term “gene” denotes a polynucleotide sequence which codes for a polypeptide in full or in part comprising introns and exons, and an open reading frame (ORF) to enable transcription. The term code denotes the ability of a nucleotide sequence to act as a template for translation, whereby the arrangement of nucleotides represents codons which further represent amino acids. A gene may further comprise additional genetic elements such as a promoter, repressor, terminator, enhancer and/or transcription factor binding elements. A gene may be inserted into the genome of an organism using genetic engineering methods known in the art, such as transformation. A gene may be exogenous (i.e. not native, inserted into the existing genome) or endogenous (i.e. exists within the genome as a native gene). | [0058] The polypeptide of the invention may be a fusion protein. A fusion protein is a polypeptide which derives from a single nucleotide sequence which contains two ormore genes or portions of genes, wherein the genes code for separate polypeptides which would not natively be transcribed and translated together. | [0059] Typically, the polynucleotide of the invention comprises a promoter, a start codon, a sequence encoding an N terminal signal peptide, a sequence encoding a protein with carbonic anhydrase activity, optionally a sequence encoding a C terminus peptide which targets the polypeptide to a further specific location e.g. anchoring in the plasma membrane, a stop codon and a terminator, as typified in Figure 3. | [0060] The coding sequence of the carbonic anhydrase encoded in the DNA polynucleotide sequence of the invention may correspond to any of the polynucleotide sequences of SEQ ID NO: 1 , or SEQ ID NO: 2, or a sequence of at least 65% identity with any of said sequences; or a sequence of at least 70% identity with any of said sequences; or a sequence of at least 80% identity with any of said sequences, or at least 85%, at least 90%, or at least 95%, identity with any of said sequences. In some embodiments, the carbonic anhydrase will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity. | [0061] The amino acid sequence of the carbonic anhydrase encoded in the polynucleotide sequence(s) of the invention may correspond to any of the amino acid sequences of SEQ ID NO: 8, or SEQ ID NO: 9, or a sequence of at least 65% identity with any of said sequences; or a sequence of at least 70% identity with any of said sequences; or a sequence of at least 80% identity with any of said sequences, or at least 85%, at least 90%, or at least 95%, identity with any of said sequences. In some embodiments, the carbonic anhydrase will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity, preferably in the extracellular root environment. | [0062] The polynucleotide may correspond to a full-length carbonic anhydrase, or a portion thereof. The term “portion”, “variant”, “homolog” or other representative wording in the art as used herein used in relation to a carbonic anhydrase sequence, or a functional fragment thereof, means any carbonic anhydrase ortholog of a differing polynucleotide or polypeptide sequence from any species, including plants.In terms of percentage identity to a reference sequence, such as SEQ ID N0:1 , 2, 8 or 9 a variant of a carbonic anhydrase may have, in increasing order of preference, at least 65%, at least 66%, at least 67%, at least 68%, at least 69%, at least 70%, at least 71 %, at least 72%, at least at least 73%, at least 74%, at least 75%, at least 76%, at least 77%, at least 78%, at least 79%, at least 80%, at least 81 %, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91 %, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, or at least 99% overall sequence identity to that reference sequence. | [0063] Carbonic anhydrases are enzymes which catalyse the reversible conversion of water (H2O) and carbon dioxide (CO2) into bicarbonate (HCO3 ) and hydrogen (H+), as detailed below:- | [0064] H2O + CO2 « HCO3- + H+| [0065] In the absence of carbonic anhydrase enzyme activity the pH of the aqueous environment determines whether the forward or backward reaction is preferred. Carbonic anhydrases are widely distributed in all organisms. Carbonic anhydrases alter the rate at which this reaction occurs and the equilibrium between CO2 and HCOs' . Carbonic anhydrases from different species may have minimal sequence similarity but can adopt similar tertiary structures to catalyse this reaction in very different contexts. | [0066] In some embodiments, the carbonic anhydrase may be an a, (3, y, 5, q, 9, or i subtype carbonic anhydrase, and in some embodiments it is a monomer. Three classes of carbonic anhydrases natively exist in plants; a, [3 and y subtypes. The [3 subtypes are better characterised and include isoforms with high efficiency for CO2 hydration; for example, [3 subtypes function as part of C4 photosynthesis in C4 plants. [3 subtypes are dimeric, whilst a subtypes are monomeric. Monomeric subtypes have the advantage that there is no requirement for multimer formation at the surface of the cell.The carbonic anhydrase sequence used in this invention may be a homolog, analog, ortholog, or paralog of any subtype of carbonic anhydrase isolated from any species. It would be expected by a person of ordinary skill in the art that any carbonic anhydrase enzyme would work equivalently in this invention, so long as it was suitable for expression by the plants of the invention (for example it consisted of naturally occurring amino acids in protein form). The Examples of the present application demonstrate that sequence identity or similarity between carbonic anhydrases is not required in order for plants of the invention to exhibit their surprising ability to sequester CO2. As noted above, carbonic anhydrases from different species can adopt similar tertiary structures regardless of sequence similarity. The skilled person would therefore understand that a plant of the invention overexpressing any type of carbonic anhydrase in the extracellular environment of the root cells would function to sequester CO2. The skilled person understands carbonic anhydrases are defined by their function. As such, any enzyme that catalyses the interconversion of gaseous CO2 and water (H2O) into ions of bicarbonate (HCO3 ) and hydrogen ions (H+) is envisaged as a carbonic anhydrase protein as part of the invention. | [0067] In some embodiments, a carbonic anhydrase with high catalytic efficiency in the direction of bicarbonate formation is selected, such that the reverse reaction would not be favored. A carbonic anhydrase may be selected based on efficacy, for example, determined via an enzyme activity assay. In addition, codon usage may be altered to enhance expression for a particular plant species. | [0068] In some embodiments, in any aspect of the invention herein defined, the promoter is a root cell specific promoter (i.e. a root cell specific promoter, or a promoter that is expressed in root cells). A promoter active in root cells is a promoter which is presently enabling expression of a polynucleotide sequence in a root cell, i.e. it is sufficient for protein production in root cells. The promoter may be active in other cells of the plant, and in some embodiments comparatively greater in root cells. The activity of the promoter may be enhanced when compared to a wild-type promoter. The activity of the promoter may be conditionally enhanced. The promoter may be an inducible promoter. The activity of the promoter may vary, such as seasonally, diurnally or in response to an external signal, i.e. temperature, pH, nutrient content of the soil. The promoter may be constitutively active.The promoter may be a synthetic promoter comprised of various selected elements. For example, such a synthetic promoter may comprise root cell specific transcription factor binding element upstream of a promoter element. There may be two or more transcription factor binding elements which may be the same or different. A plurality of such transcription factor binding elements may serve to enhance the activity and/or specificity of the promoter in root cells. The promoter may be derived from non-plant organisms, such as the 35S promoter. | [0069] In other aspects, the root cell specific promoter may be derived from a gene that is expressed preferentially or specifically in root cell of plants and therefore is a naturally occurring promoter. The gene may be expressed in other plant cell types at endogenous levels. The promoter may be selected based on its predicted function in a particular species. A person of skill in the art is well aware of many root cell specific promoters. The root cell specific promoter may be active in some or all other plant cells at some expression level but be highly expressed in the roots. | [0070] The root specific promoter encoded in the DNA polynucleotide sequence of the invention may correspond to any of the polynucleotide sequences of SEQ ID NO: 6, or SEQ ID NO: 7, or a sequence of at least 65% identity with any of said sequences; in some embodiments a sequence of at least 70% identity with any of said sequences; and in some embodiments a sequence of at least 80% identity with any of said sequences, or at least 85%, at least 90%, at least 95%, identity with any of said sequences. In some embodiments, the encoded carbonic anhydrase will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity. | [0071] The polynucleotide may correspond to a full-length root specific promoter, or a portion thereof. As mentioned above, it would be expected by a person of ordinary skill in the art that any promoter active in the roots of plants would work equivalently in this invention. | [0072] The term “portion”, “variant”, “homolog” or other representative wording in the art as used herein used in relation to a root specific promoter sequence, or a functionalfragment thereof, means any root specific promoter ortholog of a differing polynucleotide or polypeptide sequence from any species, including plants. | [0073] In terms of percentage identity to a reference sequence, such as SEQ ID NO:6 or 7, a variant of a root specific promoter may have, in increasing order of preference, at least 65%, at least 66%, at least 67%, at least 68%, at least 69%, at least 70%, at least 71 %, at least 72%, at least at least 73%, at least 74%, at least 75%, at least 76%, at least 77%, at least 78%, at least 79%, at least 80%, at least 81 %, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91 %, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, or at least 99% overall sequence identity to that reference sequence. | [0074] In one embodiment a plant whose heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells is provided wherein the gene encoding a transportable carbonic anhydrase protein comprises SEQ ID NO: 1 or SEQ ID NO: 2 or a sequence having at least 65% identity to SEQ ID NO: 1 or SEQ ID NO: 2, optionally wherein the promotor comprises SEQ ID NO: 6 or SEQ ID NO: 7 or a sequence having at least 65% identity to SEQ ID NO: 6 or SEQ ID NO: 7. | [0075] In one embodiment a plant whose heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells is provided wherein the gene encoding a transportable carbonic anhydrase protein comprises SEQ ID NO: 1 or SEQ ID NO: 2 or a sequence having at least 65% identity to SEQ ID NO: 1 or SEQ ID NO: 2, optionally wherein the promotor comprises SEQ ID NO: 6 or SEQ ID NO: 7 or a sequence having at least 65% identity to SEQ ID NO: 6 or SEQ ID NO: 7; and wherein the signal peptide sequence comprises SEQ ID NO: 3 or SEQ ID NO: 4 or a sequence having at least 65% identity to SEQ ID NO: 3 or SEQ ID NO: 4. | [0076] The root cell specific promoter may be ubiquitously active in all plant cells at endogenous levels. Endogenous levels of carbonic anhydrase mRNA and full-length polypeptide are lower in cells which are not root cells. The expression level of carbonicanhydrase may exceed endogenous levels in any biological context whereby carbonic anhydrase is expressed. The biological context may be in response to a change in the environment. | [0077] The term secreted is used to describe the transport of a protein from the inside to the outside of a cell. It is used interchangeably with transported or exported. Thus a secretable/transportable carbonic anhydrase is capable of being secreted/transported to the extracellular environment. In some embodiments, the carbonic anhydrase is transported across the plasma membrane via the secretory pathway. Secretory pathways can be conventional or non-conventional. In some embodiments, the carbonic anhydrase is transported through the conventional secretory pathway, resulting in transport of the carbonic anhydrase across the cell membrane at the cell periphery. Non-conventional transport of proteins such as carbonic anhydrase can occur through one of four pathways; direct protein translocation across the plasma membrane through membrane transport proteins, lysosomal secretion, exosome release and blebbing. Transport of the carbonic anhydrase may be active or passive. A secreted protein such as the carbonic anhydrase of the invention is in some embodiments located to the plasma membrane (also known as the extracellular membrane) in a cell. The carbonic anhydrase may be in contact with the extracellular membrane via an extracellular matrix protein such as a glycoprotein, such as extensin, or via a polysaccharide. Suitable glycoprotein and polysaccharide anchors are well known in the art. The carbonic anhydrase may be in contact with the plasma membrane via a molecular anchor such as a transmembrane domain, transmembrane helix, or a glycosylphosphatidylinositol (GPI) anchor, or other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. The carbonic anhydrase may be in contact with the plasma membrane via part of the carbonic anhydrase polypeptide of the invention, wherein part of the polypeptide represents a transmembrane protein. There may be one or more transmembrane domains. The carbonic anhydrase may not be in contact with the plasma membrane. The secreted/transported carbonic anhydrase may be adjacent to the plasma membrane or within the extracellular environment in close proximity of the plasma membrane, such as within the cell wall region. The carbonic anhydrase may remain in close proximity to the plasma membrane, but beyond the cell wall region. In some embodiments, the carbonic anhydrase is secreted into theimmediate environment surrounding the roots, such as soil or alternative bedding medium, when the plant is present in such a medium. In some embodiments, the carbonic anhydrase is not secreted within a plant nodule. The carbonic anhydrase may continue to be secreted/transported in ex vivo/ex planta when the plant is separated from another part of itself, i.e. a cutting. The secreted/transported carbonic anhydrase may diffuse out into the extracellular environment or remain on the root surface once secreted. The carbonic anhydrase secreted from the root cells may diffuse to other tissue or cell extracellular environments, such as those adjacent to root cells. This may include any cell in close proximity with the roots or the rhizophere. | [0078] The carbonic anhydrase may be released from the cell via a non-secretable pathway, such as apoptosis, or any physical interference with the cell membrane which exposes intracellular carbonic anhydrase to the extracellular environment. | [0079] The carbonic anhydrase may be over-expressed in the extracellular environment of the root cells in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells. | [0080] The term “over-expressed” regarding carbonic anhydrase refers to the expression level of carbonic anhydrase protein produced in comparison to endogenous baseline expression. The term “produced” is understood to refer to the production of the carbonic anhydrase protein and may be used interchangeably with the term expressed. Plants whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells will exhibit endogenous levels of carbonic anhydrase in all biological contexts and these levels of carbonic anhydrase will be used as a baseline comparison for the plants of the invention. Baseline levels of carbonic anhydrase typically reflect endogenous levels of carbonic anhydrases which may fluctuate according to the internal and external environment of a plant. Increased levels of carbonic anhydrase, i.e. any amount above baseline, will be considered to denote over-expression of the carbonic anhydrase protein. In some embodiments, the plant of the invention expresses 0.005%, 0.1 %, 0.5%, 1 %, 2%, 3%, 4%, 5%, 10%, 25%, 50%, 75%, 100%or 200% additional carbonic anhydrase protein in comparison to endogenous baseline expression. Endogenous baseline expression may be established in a control plant which may be a wild-type plant. Cells of the same type and morphology in the same location of the plant, i.e. root cells should be compared to one another. | [0081] A plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells is a plant which lacks a gene in its genome which encodes for a transportable carbonic anhydrase protein under the control of a promoter which is active in root cells. This plant has not been modified in the same fashion as the plants of the invention. This plant may be known as an untransformed plant, compared to a transformed plant of the invention. The plant may comprise other genetically modified elements related to or unrelated to carbonic anhydrases which are distinct from those of the invention. A plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells may be referred to or used as a “control” plant. Accordingly, the control plant has not been genetically modified to alter expression of the polynucleotide and/or polypeptide disclosed herein. This plant will exhibit endogenous levels of carbonic anhydrase in all biological contexts and these levels of carbonic anhydrase will be used as a baseline comparison for the plants of the invention. Baseline levels of carbonic anhydrase typically reflect endogenous levels of carbonic anhydrases which may fluctuate according to the internal and external environment of a plant. A control plant may be a wild-type plant. A control plant may be a wild-type plant of the same species as the plant of the invention. The control plant function is to provide a reliable reference against which the expression of polynucleotides or polypeptides of the invention can be compared against in a modified plant material. The plant of the invention may therefore be genetically engineered compared to a non-engineered plant. The control plant may be defined by determining the level of carbonic anhydrase activity by enzyme assays known in the art and defined herein. Carbonic anhydrase activity may be undetectable or at very low levels in a control plant when compared with the plant of the invention. A plant of the invention exhibits increased levels of carbonic anhydrase activity, i.e. any amount above of increased activity as compared to a control plant. Typically, a more than two-fold increase in carbonic anhydrase activity is observed in the plant of the invention compared to a control or unmodifiedplant. In some embodiments, the plant of the invention has more than a two-fold, threefold, four-fold or five-fold increase in carbonic anhydrase activity compared to a control plant. In some embodiments, the plant of the invention has more than a 0.005%, 0.1 %, 0.5%, 1 %, 2%, 3%, 4%, 5%, 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90% or 100% increase in carbonic anhydrase activity compared to a control plant. The carbonic anhydrase activity may be measured in the root cells, the whole root or whole plant. In some embodiments, the plant of the invention has more than a two-fold, threefold, four-fold or five-fold increase in carbonic anhydrase activity in the extracellular space compared to a control plant. In some embodiments, the carbonic anhydrase activity is quantified using the Wilbur-Anderson Units (WA) equation, or carbonic anhydrase esterase activity measured by the rate to catalyze hydrolysis of p- Nitrophenol acetate (pNPA) to known concentration of p-Nitrophenol (pNP) per unit of time which can alternatively be expressed in enzyme activity units such as katal (kat) or international units (IU), or carbonic anhydrase activity measured by units of conductivity changed per unit time, or carbonic anhydrase activity quantified using radiotracer based assays where activity is reported in counts or disintegrations per unit of time, or other equivalent methods to quantify carbonic anhydrase activity which is well understood by the skilled person. Optionally, the plant of the invention has a two-fold, three-fold, four-fold or five-fold increase in carbonic anhydrase activity in WA units compared to a control plant. | [0082] The gene encoding the transportable carbonic anhydrase protein may further comprise a signal peptide sequence for directing transport of the carbonic anhydrase into the extracellular environment of the plant root. The term “signal peptide” may also be known as a signal sequence, targeting signal, localization signal, localization sequence, transit peptide, target peptide, leader sequence or leader peptide. The signal peptide is usually present at the N-terminal of a polypeptide but may be present at the C-terminus. In the present invention, the signal peptide is present at the N-terminus. | [0083] Membrane-bound proteins can be type I or II; type I membrane-bound proteins rely on a signal peptide which directs them towards the secretory pathway which is subsequently cleaved, whereas type II proteins are targeted to the secretory pathwayvia their first transmembrane domain, which is not cleaved. Therefore, the signal peptide of the invention may or may not include a transmembrane domain. | [0084] The signal peptide sequence encoded in the DNA polynucleotide sequence of the invention may correspond to any of the polynucleotide sequences of SEQ ID NO: 3, or SEQ ID NO: 4, or a sequence of at least 65% identity with any of said sequences; in some embodiments a sequence of at least 70% identity with any of said sequences; and in some embodiments a sequence of at least 80% identity with any of said sequences, or at least 85%, at least 90%, at least 95%, identity with any of said sequences. In some embodiments, the carbonic anhydrase encoded from the above DNA sequences will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity. | [0085] The polynucleotide may correspond to a full length signal peptide, or a portion thereof. | [0086] The term “portion”, “variant”, “homolog” or other representative wording in the art as used herein used in relation to a signal peptide sequence, or a functional fragment thereof, means any signal peptide sequence of a differing polynucleotide or polypeptide sequence from any species, including plants. | [0087] In terms of percentage identity to a reference sequence, such as SEQ ID NO:3 or 4, a variant of a signal peptide sequence may have, in increasing order of preference, at least 65%, at least 66%, at least 67%, at least 68%, at least 69%, at least 70%, at least 71 %, at least 72%, at least at least 73%, at least 74%, at least 75%, at least 76%, at least 77%, at least 78%, at least 79%, at least 80%, at least 81 %, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91 %, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, or at least 99% overall sequence identity to that reference sequence. | [0088] The signal peptide sequence cooperates with the promoter to ensure extracellular expression and transport of the polypeptide sequence to the extracellular environment. | [0089] Also provided herein is a polynucleotide sequence comprising:• a suitable promoter; | [0090] • a sequence coding for a polypeptide sequence under the control of said suitable promoter; and | [0091] • a sequence encoding a signal peptide sequence; wherein the polypeptide sequence comprises a carbonic anhydrase sequence, and wherein the promoter is active in plant roots and capable of driving overexpression of the carbonic anhydrase, the signal peptide sequence being capable (prior to removal) of directing transport of the carbonic anhydrase into the extracellular environment of a plant root. | [0092] A suitable promoter is a promoter which enables the expression of a polypeptide sequence to which it is associated. The signal peptide sequence is sufficient to enable transport of the carbonic anhydrase into the extracellular environment of a plant root. | [0093] The signal peptide sequence may either be natively encoded or translationally fused to the carbonic anhydrase sequence to ensure transport of the carbonic anhydrase to the extracellular environment of the plant root. | [0094] The signal peptide sequence for directing transport may be derived from a secreted protein that is transported to the extracellular environment by a protein secretion pathway, and in some embodiments the conventional (or canonical) protein secretory pathway. The signal peptide sequence may be derived from the extensin protein, and in some embodiments it is derived from a carrot plant or derived from the vacuolar sorting protein, or it may be derived from a pea plant. | [0095] The plant or polynucleotide according to the invention may have a promoter, and/or a signal peptide sequence derived from a gene from the same plant species or variety as the plant. The plant or polynucleotide according to the invention may have a promoter and/or a signal peptide sequence derived from a gene from a different plant species, cultivar or variety as the plant. Plant varieties are genetic variations of the same species of plant which arise naturally in the environment. Cultivars are genetic variations of the same species of plant which have been develop by humans through controlled breeding.The promoter sequence, signal peptide sequence, transmembrane sequence and any other sequences present in the polynucleotide may be derived from any species, variety or cultivar. | [0096] The promoter of the invention is active in plant tissues that function as roots, and in some embodiments may be root hair cell and/or root epidermal cell specific. Rootspecific cells are those cells part of the root system of a plant, which may function in a root specific capacity, i.e. anchorage, stability, shelter, nutrient harvesting and storage, water absorption, transport of macromolecules. Underground stems (such as tubers, rhizomes, bulbs, corms, stolons, taro and other plant associated organs which reside underground near the roots) provide similar subterranean functions to botanically-defined root tissues and for the purposes of this invention may be considered as plant tissues that function as roots and comprise root cells. | [0097] The carbonic anhydrase may further comprise a transmembrane domain and/or a membrane anchor sequence. The transmembrane domain sequence may be a full length transmembrane domain sequence or a portion thereof. The transmembrane sequence may encode a transmembrane domain which is partially present in the plasma membrane once transported, or it may span the entire plasma membrane. The transmembrane sequence may comprise post-translational elements such as glycoproteins and polysaccharide structures. In some embodiments, the carbonic anhydrase may be attached to the outside of the cell or to the plasma membrane by a transmembrane domain, or a transmembrane helix, or a membrane anchor, or a glycosylphosphatidylinositol (GPI) anchor, or any other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. | [0098] In some embodiments, the transmembrane domain is derived from Pisum sativum BP80. The transmembrane domain sequence encoded in the DNA polynucleotide sequence of the invention may correspond to polynucleotide sequence SEQ ID NO: 5., or a sequence of at least 65% identity with any of said sequences; in some embodiments a sequence of at least 70% identity with any of said sequences; and in some embodiments a sequence of at least 80% identity with any of said sequences orat least 85%, at least 90%, at least 95%, identity with any of said sequences. In some embodiments, the carbonic anhydrase will have any of the % homologies referred to herein and retain the carbonic anhydrase enzymatic activity. | [0099] The polynucleotide may correspond to a full-length transmembrane sequence, or a portion thereof. Additionally, the polynucleotide may comprise a sequence that is capable of directing the formation of a glycosylphosphatidylinositol (GPI) anchor, or any other biomolecule which causes the carbonic anhydrase to remain attached to the plasma membrane or cell wall following secretion from the cell. | [0100] The term “portion”, “variant”, “homolog” or other representative wording in the art as used herein used in relation to a transmembrane sequence, or a functional fragment thereof, means any transmembrane sequence ortholog of a differing polynucleotide or polypeptide sequence from any species, including plants. | [0101] In terms of percentage identity to a reference sequence, such as SEQ ID NO:5, a variant of a transmembrane sequence may have, in increasing order of preference, at least 65%, at least 66%, at least 67%, at least 68%, at least 69%, at least 70%, at least 71 %, at least 72%, at least at least 73%, at least 74%, at least 75%, at least 76%, at least 77%, at least 78%, at least 79%, at least 80%, at least 81 %, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91 %, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, or at least 99% overall sequence identity to that reference sequence. | [0102] In some embodiments, the membrane anchor sequence corresponds to an entire glycophosphatidylinositol anchor sequence, or a portion thereof. | [0103] Also provided herein is an isolated polynucleotide sequence of the invention which may be fused to another polynucleotide sequence or to a targeting peptide sequence or to a transmembrane domain sequence. The polynucleotide may also be described as being engineered or non-naturally occurring.Also provided herein is an isolated polypeptide of the invention which may be fused to another polypeptide or to a targeting peptide or to a transmembrane domain. An isolated polynucleotide or polypeptide is a DNA or protein construct which exists on its own separate from the internal environment of the cell. These may comprise DNA or protein associated elements. These can be recombinant. The polypeptide of the invention may transiently comprise a signal peptide, which is subsequently cleaved upon entering the secretory pathway. The polypeptide of the invention may also comprise a signal peptide which represents a first transmembrane domain which acts as a signal peptide, which is not cleaved upon entering the secretory pathway. | [0104] Also provided herein are plant cells, cell lines or progeny thereof comprising the polynucleotide sequence or polypeptide sequence disclosed herein. The term “plant” encompasses whole plants, ancestors and progeny of the plants and plant parts, including seeds, fruit, shoots, stems, leaves, roots (including tubers), flowers, and tissues and organs, wherein each comprise the polynucleotide of the invention. The term "plant" also encompasses plant cells, suspension cultures, callus tissue, embryos, meristematic regions, gametophytes, sporophytes, pollen and microspores, wherein each comprise the polynucleotide of the invention. | [0105] In some embodiments, the plant is a crop, and in some embodiments a row or cover crop. In some embodiments the plant is selected from a corn, soybean, fava bean, mung bean, adzuki bean, broad bean, pea, cowpea, cotton, canola, camelina, potato, tomato, sugar beet, cassava, yam, sweet potato, alfalfa, wheat, barley, sorghum, oat, sorghum, millet, rye, teff, triticale, miscanthus, sorghum rice, or clover, cress, brassicas (such as Brassica oleracea), vetch and prairie grasses (such as switchgrass). | [0106] The plant may be a tree. In some embodiments the tree is poplar, spruce, pine, eucalyptus, oil palm or rubber, particularly those popular in forestry and land management, food production, carbon capture and biofuel or biomass production. | [0107] The plant may be an aquatic or a semi-aquatic plant. In some embodiments, such plants may be duckweed, mangroves, nymphaeales, or rice.The plant, polypeptide, polynucleotide, cell, cell line or progeny of the invention may sequester more carbon into the extracellular environment of the plant in comparison to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells. Sequestration of carbon occurs via the conversion of CO2 into bicarbonate and hydrogen ions. | [0108] Also provided herein are plant parts, plant tissues, plant organs, plant cells, plant protoplasts, embryos, callus cultures, pollen grains or seeds, derived or obtained from the plant of the invention. | [0109] Also provided herein are vectors comprising the polynucleotide sequence of the invention. In some embodiments, the vector is a plasmid. The plasmid may comprise an origin of replication, a T-DNA right border repeat of a Ti or Ri plasmid, a left border repeat of a Ti or Ri plasmid and at least one bacterial selectable marker. The plasmid may also comprise an enhancer, a plant selectable marker, a multicloning site and/or a recombination site. | [0110] Compositions for transformation of plant cells comprising the polynucleotide of the invention or the vector comprising the polynucleotide of the invention are also provided herein. The vector may comprise microparticles coated with said polynucleotide or said vector. | [0111] Transformation of plants is a routine technique in many species. Any of several transformation methods may be used to introduce a gene of interest into a suitable ancestor cell. According to the various aspects of the invention, the polynucleotide of the invention is introduced into a plant and expressed as a transgene through transformation. The term "introduction" or "transformation" as referred to herein encompasses the transfer of an exogenous polynucleotide into a host cell, irrespective of the method used for transfer. The methods described for the transformation and regeneration of plants from plant tissues or plant cells may be utilized for transient or for stable transformation. Transformation methods include the use of liposomes, electroporation, chemicals that increase free DNA uptake, injection of the DNA directly into the plant, floral dipping, biolistics, transformation using viruses or pollen andmicroinjection. Methods may be selected from electroporation, microinjection, RNA- coated particle bombardment or viral transfection, but are not limited to those methods recited here. The transformation method is usually dependent on the species of choice. The polynucleotide may be transiently or stably introduced into a host cell and may be maintained non-integrated, for example, as a plasmid. Alternatively, it may be integrated into the host genome. The resulting transformed plant cell may then be used to regenerate a transformed plant. To select transformed plants, plant material obtained in the transformation is, as a rule, subjected to selective conditions so that transformed plants can be distinguished from untransformed plants. For example, seeds obtained in the above-described manner can be planted and, after an initial growing period, subjected to a suitable selection and screening. | [0112] Also provided herein are bacteria comprising the polynucleotide of the invention, or a vector comprising the polynucleotide of the invention. In some embodiments, the bacterium is E coli. or Agrobacterium sp., and in some embodiments A. tumefaciens. Any suitable cloning system may be used. Genetically modified plants, including crop plants, are in some embodiments produced via Agrobacterium tumefaciens mediated transformation. Such routine methods are also used to introduce gene editing proteins such as CRISPR-Cas nucleases and base editors, which can be used to edit native carbonic anhydrase sequences to be transportable and be increased in expression in root cells. | [0113] Also provided herein are plants comprising the polynucleotide of the invention whereby the polynucleotide is stably integrated into the genome thereof; and in some embodiments heritably integrated into the genome thereof. | [0114] Methods of producing the plant or seed of the invention are also provided, comprising the steps of:- | [0115] (a) providing a vector comprising the polynucleotide of the invention; | [0116] (b) activating the promoter operably linked to the polypeptide coding DNA;| [0117] (c) optionally wherein the polypeptide is overexpressed in the extracellular environment of the cell in comparison to a plant whose heritable geneticmaterial does not comprise a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells. | [0118] A method for increasing the capacity of a plant to sequester carbon in the soil, the method comprising altering the heritable genetic material of the plant such that a carbonic anhydrase protein is transported from the roots of the plant into the extracellular environment is also provided. The normal capacity of a plant to sequester carbon in the soil is indicated by a plant which has not been genetically modified in the same way as a plant of the present invention. This capacity may reflect the uppermost limit of the rate of conversion of CO2 into bicarbonate and hydrogen ions in the extracellular environment of plants which have not been genetically modified in the same way as a plant of the present invention. This rate achieved in the modified plants is inherently dependent upon the transport of carbonic anhydrase from the roots of the plant into the extracellular environment. The altering of heritable genetic material may comprise inserting at least one polynucleotide into the heritable genetic material of a plant cell using methods of transgenic manipulation is well known in the art. | [0119] The altering of heritable genetic material may also comprises genetically editing the heritable genetic material of a plant cell, using methods of genetic modification well known in the art, such as CRISPR, TALENs and meganucleases. Base editing may also be used, whereby a single nucleotide can be manipulated in a targeted gene. Prime editing may also be used, which is a search-and-replace genome editing method used to insert precise, small indels including single or multiple base substitutions, transitions and transversions without requiring double stranded breaks and donor repair templates. Any regulatory sequence may also be manipulated using these techniques to result in increased expression of the carbonic anhydrase, for example, by introducing random indels into a native regulatory sequence using a CRISPR-Cas system. | [0120] Any polynucleotides disclosed herein may further include a polynucleotide sequence encoding a CRISPR-Cas protein, optionally a guide RNA (gRNA), wherein the gRNA directs the CRISPR-Cas protein to the locus of at least one copy of an endogenous carbonic anhydrase gene thereof in the plant cell genome, whereby a root-specificpromoter is inserted so as to cause expression of the copy or copies of the carbonic anhydrase in at least some root cells of the plant. | [0121] A native carbonic anhydrase may also be manipulated using gene editing tools to introduce a signal peptide to a native carbonic anhydrase gene using targeted nucleases and homology directed repair or non-homologous end joining repair mechanisms and a template sequence containing the signalling peptide. Such gene knock in techniques are well known in the art. Also provided herein are processed plant products obtained from the plant or the plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus culture, pollen grain or seed disclosed herein. The processed plant product may comprise a detectable nucleic acid sequence of (i) a transportable carbonic anhydrase downstream of a gene expression regulatory element active in at least some of the root cells of a plant, or (ii) a polynucleotide or at least a portion of a polynucleotide of the invention which is present in the product. Processing may involve chemical or physical manipulation of the product in order to form a product with desirable properties suited to a particular function, i.e. pelleting.| [0122] EXAMPLES | [0123] Example 1 | [0124] To demonstrate that plant roots can be engineered to produce active carbonic anhydrase protein a soybean (Glycine max) carbonic anhydrase gene was selected for overexpression (accession number Glyma.19G135900 [SEQ ID NO: 1 and SEQ ID NO: 8]). This carbonic anhydrase has an annotated ‘Eukaryotic-type carbonic anhydrase’ domain (Pfam #PF00194.24) in its protein sequence. | [0125] The expression of the carbonic anhydrase gene (SEQ ID NO: 1 and SEQ ID NO: 8) was placed under the control of a 35S promoter and cloned into the pCAM BIA-1300 plant expression vector. This vector included a herbicide resistance gene (kanamycin) and the expression cassette was flanked by agrobacterium LB and RB t-DNA sequences. The vector was transformed into Agrobacterium rhizogenes strain K599 using electroporation and this was used to transform soybean roots using a hairy root transformation method according to the protocols in (Chen et al., 2018). | [0126] Following transformation positively transformed root tissue was identified visually by the expression of a visual reporter. Root tissue was isolated from transformed roots and equivalent non-transformed root tissue was sampled as a control. Root tissue was homogenised in in 700pl of extraction buffer in a chilled pestle and mortar. Homogenised root was transferred to 2ml tube and centrifuged for 15mins at 5000rpm at 4C. All assays were performed on the supernatant following this spin step. | [0127] A carbonic anhydrase assay was carried out to measure carbonic anhydrase activity. This assay measures the rate of change in pH of CO2-saturated water following the addition of root homogenate from transformed and untransformed (also known as wild type control) root tissue. The pH change results from the release of protons (H+) by carbonic anhydrase. Change in pH is directly proportional to the amount of bicarbonate that has been produced by carbonic anhydrase. Such assays are known to those familiar with the art. | [0128] For each carbonic anhydrase assay 10OpI of supernatant from the homogenised root samples was used. For a no-root tissue control, 1 OOpI of extraction buffer without roottissue was used. Samples were added to 2ml tube containing 1100pl of a 20 mM Tris- HCI solution at pH 8.3 containing 0.003% bromothymol blue. Following this, 800pl of ice chilled CO2 saturated water was added. The time taken to change colour from blue (pH 8.3) to yellow (pH 5.3) was recorded. All reactions were performed on ice. | [0129] The Wilbur-Anderson Units (WA) equation was used to calculate activity: | [0130] WA units = (tO-ts)Zts where to is the time taken for the colour change to occur in the no-root control reaction and fs is the time taken for the colour change to occur in samples containing supernatant from the homogenised root. | [0131] Carbonic anhydrase activity was significantly increased at ~2x higher in the transgenic root samples compared to the wild type root samples (P=0.022669, one-tailed Student’s t-test, unequal variance) (Figure 2A). Thus, soybean root cells can be engineered to have increased carbonic anhydrase activity through the overexpression of a gene encoding a carbonic anhydrase protein, and this protein is catalytically active when released from root cells into an extracellular environment. | [0132] Example 2 | [0133] In order for carbonic anhydrase to facilitate conversion of CO2 to HCO3 in the extracellular environment of the plant they need to be secreted/transported from the cells of the plant into the extracellular environment. There are several mechanisms by which cells target proteins for secretion/transport from the cell into the extracellular environment. The two main ways in which this is achieved are the conventional secretory pathway and the unconventional secretory pathway. The conventional secretory pathway achieves protein secretion/transport through the use of N-terminal signal peptides. | [0134] To demonstrate that carbonic anhydrase proteins can be engineered to be secreted/transported from plant cells we translationally fused an experimentally characterised signal peptide from the carrot (Daucus carota) extensin gene (G. Li et al., 2009) [SEQ ID NO: 3] with the soybean carbonic anhydrase provided in Example1 [SEQ ID NO: 1 and SEQ ID NO: 8], This fusion protein was placed under the control of a root specific promoter from the soybean expansin gene (Glyma.17G133100) [SEQ ID NO:6], and cloned into a plant transformation vector that also included a herbicide resistance gene (spectinomycin) and was flanked by agrobacterium LB and RB t-DNA sequences (Figure 1 ). The vector was transformed into Agrobacterium tumefasciens (LBA4404 strain) by electroporation, positive colonies were selected and cultured using standard techniques. To demonstrate that this technology would have broad utility in all plant species, this vector was transformed into Arabidopsis thaliana using floral dip method (Clough & Bent, 1998) and stable transgenic lines were generated. | [0135] It should be noted that although the soybean expansin gene promoter was used in this example, other root promoters are known in the art (for example (Y. Li et al., 2019; Marques-Bueno et al., 2016). It would be expected by those of ordinary skill in the art that any root promoter selected from any species would be expected to function equivalently to drive expression in roots. It should also be noted that the technology of the invention would be expected to work if the carbonic anhydrase protein was expressed throughout the plant, or in other plant tissues, so long as the expression domain encompassed expression in roots. | [0136] An experiment was performed to demonstrate that plants expressing secretable/transportable carbonic anhydrase in root cells resulted in carbonic anhydrase activity in the extracellular environment of the root. Here, transformed plants and wild type control plants were grown for six-weeks in hydroponic conditions. At six weeks, individual plants were transferred to 15ml of fresh hydroponic media and allowed to grow for two days. Following this two-day period, the hydroponic solution was sampled and used for carbonic anhydrase activity assays to measure the amount of carbonic anhydrase activity that had been secreted/transported from the roots into the hydroponic medium. | [0137] Here, 10OpI of hydroponic solution was added to a 2ml snap lid microcentrifuge tube containing 1050pl of a 20 mM Tris-HCI solution (pH 8.3) with 0.003% bromothymol blue and 1 OOpI extraction buffer (200mM Tris HCI pH8.3, 1 mM EDTA, 20mM MgCl2, 50mM NaCI, 100mM Na2SO4). Subsequently, 750pl of ice chilled CO2 saturated water (generated by soda stream) was added to start the reaction. The time taken for acolour change from blue (pH 8.3) to yellow (pH 5.3) was recorded and used to calculate enzyme activity as in Example 2. The reaction was performed on ice. | [0138] The carbonic anhydrase activity was significantly increased at 11x higher in the hydroponic medium samples from transgenic plants than from hydroponic medium samples from wild-type control plants (P=0.029404, one-tailed Student’s t-test, unequal variance) (Figure 2B). Thus, plants transformed with the invention successfully expressed and secreted active carbonic anhydrase protein into the extracellular environment of the root, which in turn catalysed conversion of CO2 to bicarbonate. | [0139] Example 3 | [0140] To demonstrate that this technology also works to sequester CO2 in the soil a separate experiment was performed on soil grown plants. Given that carbonic anhydrase catalyses the conversion of CO2 and water into bicarbonate and a proton, the sequestration of atmospheric CO2 in the soil is directly proportional to the pH change of the soil. Here, transgenic plants and wild type plants (described in Example 2) were grown in 6.5cm pots containing 110g Westland John Innes No.3 Mature Plant Compost for six weeks. Soil control pots not containing any plants were also constructed. For each pot, the pH of the soil 2cm below the surface was measured in three random locations using a HANNA™ soil pH tester (HI-981030). As shown in Figure 2C, the soil pH in the pots containing transgenic plants of the invention was significantly lower than either pots containing no plants (‘soil control’) (P=0.000092, one-tailed Student’s t-test, unequal variance), or pots containing wild-type plants (P=0.000449, one-tailed Student’s t-test, unequal variance). Thus, pots containing plants of the invention sequestered more CO2 in the soil than pots containing control plants or pots containing no plants. | [0141] Plants were also imaged as they grew. There were no obvious differences in the phenotype between transgenic and wild type plants across plant development, growth rate, flowering, or seed set (Figure 2F). Thus, secreting carbonic anhydrase from roots, and sequestering CO2 in the soil as bicarbonate, is not deleterious to plant growth.Example 4 | [0142] A CO2 soil flux experiment was conducted to further demonstrate that transgenic plants of the invention increased the rate at which CO2 diffuses from the air into the soil and is converted into bicarbonate. | [0143] Here, transgenic plants and wild type plants (described in Example 2) were grown in 6.5cm pots containing 110g Westland John Innes No.3 Mature Plant Compost for 6 weeks. After 6 weeks all above ground biomass (i.e. leaves, stems etc) was removed and the pot containing all of the below ground biomass in soil was placed in a LI-COR 6800 small plant chamber in complete darkness (achieved by covering chamber in tinfoil). The CO2 that was absorbed or emitted by the soil in the pot was then measured using the LI-COR 6800. To do this, the chamber was equilibrated in CO2 free air for 1 hour. After 1 hour, the CO2 level was raised to 1000 ppm (~2.5x atmospheric CO2 concentration). Following 1 minute of acclimation, the soil CO2 sequestration rate was measured every second for a 30-m inute recording window. Net carbon sequestration was calculated by summing the carbon sequestration over the recording window. As shown in Figure 2D, this revealed that pots containing control plant roots did not sequester CO2 from the air stream, and instead produced CO2 through soil respiration. In contrast, pots containing roots of transgenic plants of the invention depleted CO2 from the air stream. Thus, plants of the invention facilitated CO2 sequestration into the soil. Moreover, the magnitude of this sequestration is substantially larger than the CO2 released through soil respiration. | [0144] Example 5 | [0145] To demonstrate that other carbonic anhydrase genes from other species can be used in different embodiments of this invention we expressed a carbonic anhydrase from the diatom Conticribra weissflogii (also known as Thalassiosira weissflogii) [SEQ ID NO: 2], As above this carbonic anhydrase was translationally fused to the experimentally characterised signal peptide from the carrot (Daucus carota) extensin gene (G. Li et al., 2009) [SEQ ID NO: 3], This fusion protein was placed under the control of a root specific promoter from the soybean expansin gene (Glyma.17G133100) [SEQ ID NO:6], and cloned into a plant transformation vector that also included a herbicide resistance gene (spectinomycin) and was flanked by agrobacterium LB and RB t-DNA sequences. The vector was transformed intoAgrobacterium tumefasciens (LBA4404 strain) by electroporation, positive colonies were selected and cultured using standard techniques. This vector was transformed into Arabidopsis thaliana and stable transgenic lines were generated. | [0146] Seeds of transgenic plants expressing the secretable/transportable carbonic anhydrase from Conticribra weissflogii (SEQ ID NO 2 and 9) and seeds of wild type plants were germinated on >2 Murashige and Skoog + 1 % sucrose + 2.5mM MES agar plates. After 7 days seedlings were transferred to 96 well plates with only the roots entering each well. Each well in the 96 well plate contained 350pl of >2 Murashige and Skoog + 1 % sucrose solution and 30mg L-1 bromocresol purple. After four hours the seedlings were removed and the absorbance at 429 nm was measured using a plate reader. Carbonic anhydrase activity was estimated from the rate of change in pH over the four hour time period. The carbonic anhydrase activity was significantly higher in the root environment of the transgenic plants than in the root environment of the wildtype control plants (P=0.017435, one-tailed Student’s t-test, unequal variance) (Figure 2E). Thus, plants transformed with the secretable/transportable carbonic anhydrase from Conticribra weissflogi successfully expressed and secreted active carbonic anhydrase protein into the extracellular environment of the root, which in turn catalysed conversion of CO2 to bicarbonate. This demonstrates that carbonic anhydrase proteins from any species and any carbonic anhydrase subtype would be by expected to work equivalently. | [0147] Example 6 | [0148] To demonstrate that soybean plants can be engineered such that their roots secrete active carbonic anhydrase proteins into the extracellular environment we translationally fused an experimentally characterised signal peptide from the carrot (Daucus carota) extensin gene provided in Example 2 [SEQ ID NO: 3] with the soybean carbonic anhydrase provided in Example 1 [SEQ ID NO: 1 and SEQ ID NO: 8], This fusion protein was placed under the control of a root specific promoter from the soybean expansin gene (Glyma.17G133100) [SEQ ID NO:6], and cloned into a plant transformation vector that also included a herbicide resistance gene (spectinomycin) and was flanked by agrobacterium LB and RB t-DNA sequences (Figure 1 ). The vector was transformed into Agrobacterium tumefasciens culturedusing standard techniques. This vector was transformed into Glycine max and stable engineered lines were generated. Engineered and azygous control plants were grown for 3-weeks on Levington advance F2S Seed & Modular & Sand Compost before washing roots and transplanted to 4.5L hydroponic boxes. Plants were grown on hydroponic media for two weeks as previously described by Hata & Futamura (2020). After two weeks the hydroponic media was replenished with fresh media and plants were grown for five days depending on the rate of plants consuming hydroponic media. Samples of hydroponic media from hydroponic boxes containing either control or engineered plants were filtered through a Falcon 40pm cell strainer to remove plant debris. Proteins present in the filtered samples were then isolated and concentrated using Pierce 10kD MWCO protein concentrating column. The total protein concentration of each isolated protein sample was calculated using a Bradford Protein assay and total protein concentration adjusted to be equal across all samples. To measure Carbonic anhydrase activity an adapted version of the protocol described in Ozdemir ((2009) was used. Here, 160pl of concentrated hydroponic media samples were added to 120pl of 50mM Tris-HCI pH 7.5 in a well of a 96-well microplate. Following this, 30 I of 10mM p-Nitrophenyl acetate dissolved in acetonitrile was added to each well to start the colorimetric assay. A spectrophotometer plate reader was used to measure absorbance in each well at 400nm over a 16-hour period at 25C. Carbonic anhydrase activity was reported as pM of p-Nitrophenol synthesised per second. Mean carbonic anhydrase activity was calculated from two independent azygous lines and three independent engineered lines (Figure 4A). Protein samples isolated from hydroponic medium that contained azygous plants exhibited a baseline p-nitrophenyl hydrolysis activity. Protein samples isolated from hydroponic medium that contained engineered plants exhibited a significantly higher p-nitrophenyl hydrolysis activity. This is consistent with the presence of secreted carbonic anhydrase in the hydroponic medium that contained engineered plants. | [0149] Plants were also imaged as they grew on soil. There were no obvious differences in the phenotype between engineered soybean plants and control plants across plant development, growth rate, flowering, or seed set (Figure 4F). Thus, secreting carbonic anhydrase from roots, and sequestering CO2 in the soil as bicarbonate, was not deleterious to plant growth.Example 7 | [0150] To demonstrate that soybean plants that have been engineered to secrete active carbonic anhydrase proteins into the extracellular environment enable sequestration of CO2 in the soil the following experiment was performed. Engineered plants expressing a secretable carbonic anhydrase in root hair cells (as described in Example 6) and wild-type control plants were grown in 13cm pots containing 1 :1 :2:2 Levington M3 compost, Melcourt topsoil, Melcourt sharp sand and perlite mixed with 5ml Miracle- Gro All Purpose Continuous Release Plant Food. When plants were 17-weeks old a 2.1 cm diameter soil sampler probe was used to collect a soil core at a random location near the root zone from each pot and transferred to falcon tube. An equal volume to soil weight of ddH2O was added and mixed for 30 minutes and allowed to stand for 1- hour. Using a METLER pH probe the pH of the soil slurry was measured. The pH of the soil from the pots containing engineered plants of the invention was significantly lower (P=0.00798, one-tailed Student’s t-test, unequal variance) than pots containing wild-type plants (Figure 4B). This reduction in soil pH is consistent with the presence of active carbonic anhydrase protein, and thus an increased concentration of bicarbonate, in the soil of pots containing engineered plants of the invention. Thus, soil in which plants of the invention were grown sequestered more CO2 than soil in which control plants were grown. | [0151] Example 8 | [0152] To demonstrate that carbonic anhydrase genes from any species can be used in engineered plants of the invention the soybean carbonic anhydrase gene used in Example 1 and Example 2 above was exchanged for a carbonic anhydrase gene from a marine alga [SEQ ID NO: 2], All other components of the vector for plant transformation were kept the same. To demonstrate that the carbonic anhydrase protein that is expressed is secreted from soybean roots and is active engineered plants of the invention and azygous control plants were grown for 3-weeks on Levington advance F2S Seed & Modular & Sand Compost before washing roots and transplanting to 4.5L hydroponic boxes. Plants were supported on hydroponic media as previously described by (Hata & Futamura 2020). Plants were grown hydroponically for 1-week. Hydroponic media was then replenished with fresh media and plants weregrown for a further 7-days. Samples of media from hydroponic boxes containing only control or engineered plants was isolated and filtered through a Falcon 40pm cell strainer to remove plant debris. The proteins present in the filtered samples were then isolated and concentrated using Pierce 10kDMWCO protein concentrating column. The total protein concentration of each sample was calculated using a Bradford Protein assay and enzyme activity was normalised to total protein content. To measure Carbonic anhydrase activity an adapted version of protocol described in Ozdemir (2009). was used. Here, 160 I of concentrated hydroponic media samples were added to 120pl of 50mM Tris-HCI pH 7.5 in a well of a 96-well microplate. Following this, 30pl of 10mM p-Nitrophenyl acetate dissolved in acetonitrile was added to each well to start the colorimetric assay. A spectrophotometer plate reader was used to measure absorbance in each well at 400nm over a 11 -hour period at 25C. | [0153] As shown in Figure 4C, protein samples isolated from hydroponic medium that in which azygous plants were grown exhibited a baseline p-nitrophenyl hydrolysis activity. Protein samples isolated from hydroponic medium that in which engineered plants of the invention were grown exhibited a significantly higher p-nitrophenyl hydrolysis activity. This is consistent with the presence of secreted carbonic anhydrase in the hydroponic medium that contained engineered plants. | [0154] Example 9 | [0155] To demonstrate that soybean plants that have been engineered to express active carbonic anhydrase proteins on the surface of their roots to enable sequestration of CO2 in the soil, the following experiment was performed. As above engineered soybean plants where soybean carbonic anhydrase [SEQ ID NO: 3] was translationally fused with experimentally characterised signal peptide and transmembrane domain from pea (Pisum sativum) [SEQ ID NO: 4 and SEQ ID NO:5], This fusion protein was placed under the control of a root specific promoter from the soybean expansin gene (Glyma.17G133100) [SEQ ID NO:6], and cloned into a plant transformation vector that also included a herbicide resistance gene (spectinomycin) and was flanked by agrobacterium LB and RB t-DNA sequences (Figure 1 ). The vector was transformed into Agrobacterium tumefasciens cultured using standard techniques. This vector was transformed into Glycine max and stable engineered lines were generate. Engineeredand azygous control plants were grown in 13cm pots containing John Innes Cereal Mix. When plants were 13-weeks old a 2.1 cm diameter soil sampler probe was used to collect a soil core sample at a random location near the root zone from each pot and transferred to falcon tube. An equal volume to soil weight of ddH2O was added and mixed for 30 minutes and allowed to stand for 1 -hour. The pH of the soil slurry was measured using a METLER pH probe. As shown in Figure 4D, the pH of the soil in the pots in which engineered plants of the invention were grown was significantly lower than the pH of the soil in the pots containing wild-type plants. This reduction in soil pH is consistent with the presence of active carbonic anhydrase protein, and thus an increased concentration of bicarbonate, in the soil of pots containing engineered plants of the invention. Thus, pots containing engineered plants of the invention sequestered more CO2 in the soil than pots containing control plants or pots containing no plants. | [0156] Example 10 | [0157] To demonstrate that other carbonic anhydrase genes from other species can be engineered and localised extracellularly on root hairs of soybean roots engineered plants used in Figure 4C and their respective azygous control plants were grown for 3-weeks on Levington advance F2S Seed & Modular & Sand Compost and transplanted to 4.5L hydroponic boxes. Plants were supported on hydroponic media as previously mentioned by Hata & Futamura (2020). Plants were grown hydroponically for 2-weeks with media refreshed weekly. To measure carbonic anhydrase activity on root surface an adapted carbonic anhydrase p-nitrophenyl hydrolysis activity protocol taken from Ozdemir (2009) was used. 500mg fresh weight of soybean roots were removed were briefly washed with sterile water to remove excess hydroponic media and then placed in 30ml beaker containing 18ml 50mM Tris- HCI pH 7.5. 2ml 10mM p-Nitrophenyl acetate dissolved in acetonitrile was used to start the reaction. Absorbance of 300pl samples at 400nm was recorded at 1 -minute and 33 minutes using spectrophotometer plate reader. Carbonic anhydrase activity was reported as pM of p-Nitrophenol synthesised per second. | [0158] Engineered plant roots demonstrated significantly higher (P=0.030458, one-tailed Student’s t-test, unequal variance) p-nitrophenyl hydrolysis activity compared tocontrol plant roots (Figure 4E). This is consistent with the detection of carbonic anhydrase activity extracellularly from roots of engineered plants. | [0159] Example 11 | [0160] To demonstrate that carbonic anhydrase enzymes can be engineered to be localised extracellularly on the plasma-membrane of the cell, a reporter-gene fusion was made and tested in protoplasts. Here, Conticribra weissflogii carbonic anhydrase [SEQ ID NO: 2] was translationally fused with the coding sequence for a fluorescent protein to produce a gene-reporter fusion. This gene-reporter fusion was then translationally fused at the N-terminus and C-terminus with a signal peptide and transmembrane domain, respectively, from the pea (Pisum sativum) gene PsBP80 [SEQ ID NO: 4 and SEQ ID NO:5], This final fusion protein was placed under the control of a cassava vein mosaic virus promoter (Verdaguer et al. (1996)) and cloned into a plant transformation vector. To provide a cytoplasmic localised control, the Conticribra weissflogii carbonic anhydrase translationally fused with the coding sequence for a fluorescent protein, without the PsPB80 signal peptide and transmembrane domain, was also placed under the control of a cassava vein mosaic virus promoter (Verdaguer et al. (1996)) and cloned into a plant transformation vector. | [0161] Soybean protoplasts were transfected with these two expression vectors following the protocol by Sultana et al. (2019). After 2-days, the transfected protoplasts were imaged using a Leica TCS SP5 confocal microscope. Protoplasts expressing Conticribra weissflogii carbonic anhydrase fused to the coding sequence for a fluorescent protein, without the PsPB80 signal peptide and transmembrane domain, showed a clear cytosolic localisation (Figure 5A). In contrast, protoplasts expressing Conticribra weissflogii carbonic anhydrase fused to the coding sequence for a fluorescent protein with the PsBP80 signal peptide at the N-terminus and the PsBP80 transmembrane domain at the C-terminus localised to the plasma membrane (Figure 5B).Example 12 | [0162] To demonstrate that promoters used for generation of engineered plants herein drive expression in specific root tissues, GUS reporter lines were generated. Here, pGmEXPA7 (SEQ ID NO:6) and pGmPIN2b (SEQ ID NO:7) were each used independently to drive expression of GUS(Cat1 +) (beta-glucuronidase gene with castor bean catalase first intron Cat1 ) . These promoter-GUS fusions were separately cloned into a plant transformation vector that included a herbicide resistance gene (Kanamycin) and was flanked by agrobacterium LB and RB t-DNA sequences. The resulting vectors were transformed into Agrobacterium tumefasciens (LBA4404 strain) by electroporation and positive colonies were selected and cultured using standard techniques. These agrobacterium strains were used to transform Arabidopsis thaliana via the floral dip method (Clough & Bent, 1998). Engineered plants were germinated on >2 Murashige and Skoog + 1 % sucrose + 2.5mM MES agar plates. After 10 days, seedlings were transferred to 6-well plates and GUS histochemical staining was performed. 5ml of GUS staining buffer (0.5mM KsFe(CN)6, 0.5mM K4Fe(CN)e 3H2O, 50mM Sodium Phosphate buffer, 10mM Na2EDTA H2O, 1 mM X-Gluc and 0.1 % Triton- X (v:v)) was added to seedlings and incubated at 37C for 3-hours. Seedlings were washed and cleared with 70% ethanol overnight. Stained and chlorophyll cleared seedlings roots were imaged using an Optika B-383FL microscope combined with OneView camera and imaging software. | [0163] GUS expression driven by the pGmPIN2b promoter [SEQ ID NO:6) was localised to the epidermis of root tip and some expression extending up the primary root (Figure 5C). GUS expression driven by the pGmEXPA7 promoter was localised to the root hair cells (Figure 5D). | [0164] Example 13 | [0165] To demonstrate that engineered plants of the invention enable increased accumulation of soil inorganic carbon the following experiment was performed. Engineered plants described in Example 6 that express a secreted soybean carbonic anhydrase from root hair cells [SEQ ID NO: 6] and azygous control plants were grown in 13cm pots containing 1 :1 :2:2 Levington M3 compost, Melcourt topsoil, Melcourt sharp sand and perlite soil mixed with 5ml Miracle-Gro All Purpose Continuous Release Plant Fooduntil the end-of-life cycle. When seeds were harvested, and soil was dry, the dried biomass and roots in the soil were removed and the remaining soil was sieved through 2mm sieve. The soil samples were sent to Eurofins AgroTesting UK for soil Carbon Check to analyse soil inorganic (SIC) and organic carbon (SOC) content. | [0166] Mean inorganic carbon content of soil from pots in which engineered plants were grown was higher than soil from pots in which azygous control plants or no plants were grown (Figure 6A). | [0167] Example 14 | [0168] To demonstrate that exogenous soil treatments can be used in combination with engineered plants of the invention to enhance CO2 sequestration in the soil the following experiment was performed. Here, engineered Arabidopsis thaliana plants described in Example 2 expressing a secretable carbonic anhydrase in root hair cells and wild-type control plants were grown in 6.5cm pots containing 160g of Levington advance F2S Seed & Modular & Sand Compost mixed with 4.16g L-1 Ca(OH)2. The pH of the soil was adjusted to pH 8 to facilitate enhanced conversion of HCO3- to CO3- which can then combine with Ca from Ca(OH)2 to form CaCOs. | [0169] Plants were grown for 10-weeks. At 10 weeks, all above soil biomass was removed and the soil was sent to Eurofins AgroTesting UK for soil Carbon Check to analyse soil inorganic (SIC) and organic carbon (SOC) content. Soil in which engineered plants of the invention were grown exhibited increased soil inorganic carbon (Figure 6B) and significantly higher soil inorganic carbon normalised against soil organic carbon (P=0.002078, one-tailed Student’s t-test, unequal variance) (Figure 6C). This is consistent with the presence of carbonic anhydrase activity, and thus enhanced conversion of CO2 to bicarbonate, in the soil in which engineered plants of the invention were grown. Thus, soil treatments can be used in conjunction with engineered plants of the invention to enhance CO2 sequestration. It would be expected by those of ordinary skill in the art that any soil treatment rich in positively charge cations such as magnesium oxide or cations derived from crushed rock soil treatments or fertilizer treatments or deploying the technology on soils that are naturally richer in cations would be expected to function equivalently when used with our invention to increase inorganic soil carbon, our invention to increase inorganic soil carbon.Example 15 | [0170] To demonstrate that engineered plants of the invention enable increased accumulation of soil inorganic carbon the following experiment was performed. Engineered soybean plants described in Example 8 expressing soybean carbonic anhydrase that is anchored to the plasma membrane of root hair cells and their respective azygous control plants were grown in 13cm pots containing 1 :1 :2:2 Levington M3 compost, Melcourt topsoil, Melcourt sharp sand and perlite soil mixed with 5ml Miracle-Gro All Purpose Continuous Release Plant Food until the end-of-life cycle. When seeds were harvested, and soil was dry, the dried biomass and roots in the soil were removed and the remaining soil was sieved through 2mm sieve. The soil samples were sent to Eurofins AgroTesting UK for soil Carbon Check to analyse soil inorganic (SIC) and organic carbon (SOC) content. | [0171] Soil in which engineered plants of the invention were grown exhibited significantly increased soil inorganic carbon (P=0.032395, one-tailed Student’s t-test, unequal variance) (Figure 6D) and significantly higher soil inorganic carbon normalised against soil organic carbon (P=0.048304, one-tailed Student’s t-test, unequal variance) (Figure 6E) than soil in which control plants were grown. | [0172] This is consistent with the presence of increased carbonic anhydrase activity, and thus enhanced conversion of CO2 to bicarbonate to generate inorganic carbon in the soil in which plants of the invention were grown. Thus demonstrating engineered plants of the invention to enhance carbon sequestration in the soil. | [0173] REFERENCES | [0174] Boone, C. D., Gill, S., Habibzadegan, A., & McKenna, R. (2013). Carbonic anhydrase: An efficient enzyme with possible global implications. In International Journal of Chemical Engineering, https://d0i.0rg/l 0.1155/2013/813931| [0175] Chen, L., Cai, Y., Liu, X., Guo, C., Sun, S., Wu, C., Jiang, B., Han, T., & Hou, W. (2018). Soybean hairy roots produced in vitro by Agrobacterium rhizogenes- mediated transformation. The Crop Journal, 6(2), 162-171.Clough S. , Bent A. Floral dip: a simplified method for Agrobacterium-mediated transformation of Arabidopsis thaliana. Plant J. 1998, 16(6), 735-743. doi: 10.1046/j.1365-313x.1998.00343.x. PMID: 10069079. | [0176] DiMario, R. J., Clayton, H., Mukherjee, A., Ludwig, M., & Moroney, J. v. (2017). Plant Carbonic Anhydrases: Structures, Locations, Evolution, and Physiological Roles. Molecular Plant, 10( ), 30-46. https://doi.Org/10.1016/j.molp.2016.09.001| [0177] Hayashi, T., Shimoda, Y., Sato, S., Tabata, S., Imaizumi-Anraku, H., & Hayashi, M. (2014). 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Potential and costs of carbon dioxide removal by enhanced weathering of rocks. Environmental Research Letters, 13(3). https://doi.org/io.i088/i748-9326/aaa9c4| [0189] Sultana, S. M., Frazier, T. P., Millwood, R. J., Lenaghan, S. C., & Stewart Jr, N. C. (2019). Development and validation of a novel and robust cell culture system in soybean (Glycine max (L.) Merr.) for promoter screening. Plant Cell Reports, 38, 1329-1345. doi : https://doi . org/10.1007/s00299-019-02455-5 | [0190] Verdaguer B., de Kochko A., Beachy R. N. & Fauquet C. (1996) Isolation and expression in transgenic tobacco and rice plants, of the cassava vein mosaic virus (CVMV) promoter. Plant Mol Biol, 31 (6), 1129-39. doi: 10.1007/BF00040830. Family Number|(110665836)|110665836|Abstract|(WO2024149976 A1)|Root-specific expression of carbonic anhydrase increases the environmental carbon sequestration ability of plants. Here, a plant is genetically engineered so that its heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment. These genetically altered plants demonstrate increased levels of carbonic anhydrase activity in the extracellular environment of the plant roots, which enhances carbon sequestration in extracellular environments such as soil.|(AR-131571 A1)|Root-specific carbonic anhydrase expression increases the environmental carbon sequestration capacity of plants. Here, a plant is genetically modified such that its heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in the stem cells, such that the carbonic anhydrase is transported from the plant roots to the extracellular medium. These genetically altered plants show higher levels of carbonic anhydrase activity in the extracellular medium of plant roots, which improves carbon capture in an extracellular medium such as soil. Claim 1: An isolated polynucleotide sequence comprising a sequence encoding a polypeptide sequence under the control of a suitable promoter, wherein the polypeptide sequence comprises a carbonic anhydrase sequence and a signal peptide sequence, wherein the promoter is active in plant roots and capable of directing the over-expression of anhydrase, the signal peptide sequence capable of directing the transport of carbonic anhydrase to the extracellular medium of a plant root. Claim 9: An isolated polypeptide sequence encoded by the polynucleotide of any one of claims 1 to 8. Claim 10: A plant cell, cell line or progeny thereof unable to generate a complete individual comprising the isolated nucleotide sequence or isolated polypeptide sequence of any of claims 1 to 9. Claim 11: The isolated polynucleotide, isolated polypeptide, cell, cell line or progeny incapable of generating a complete individual according to any preceding claim, wherein the plant is a crop, preferably a row or cover crop, preferably selected from maize, soybeans, pea, cotton, rapeseed, camelina, potato, tomato, sugar beet, cassava, sweet potato, alfalfa, wheat, barley, sorghum, oats, sorghum, millet, rye, teff, rice plant, or clover, watercress, brassicaceae, vetch and prairie grasses. Claim 14: A part of the plant, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus, cell culture, pollen grain or seed, derived or obtained from a plant cell, cell line or progeny according to any of claims 10 to 13. Claim15: An isolated vector for expression in plants comprising the polynucleotide sequence of any of claims 1 to 13, wherein the vector is, optionally, a plasmid. Claim 16: A composition for the transformation of plant cells comprising the isolated polynucleotide of any one of claims 1 to 13, or the vector of claim 15; optionally comprising microparticles coated with said polynucleotide or said vector. Claim 17: A bacterium comprising the polynucleotide of any one of claims 1 to 13, or the vector of claim 15; optionally wherein the bacterium is E coli. or Agrobacterium sp., more preferably A. tumefaciens. Claim 18: A method for producing a plant or seed, comprising the steps of: (a) providing a vector of claim 15; (b) transforming a plant with the vector of claim 15; (c) activating the promoter operatively attached to the DNA encoding the polypeptide; (d) optionally, wherein the polypeptide is over-expressed in the extracellular medium of the cell compared to a plant whose heritable genetic material does not comprise a gene encoding a transportable carbon anhydrase protein under the control of a promoter active in stem cells. Claim 22: A processed plant product obtained from the plant part, plant tissue, plant organ, plant cell, plant protoplast, embryo, callus, cell culture, pollen grain or seed according to claim 14; optionally, wherein the processed product comprises a nucleic acid sequence detectable from (i) a carbonic anhydrase transportable downstream of a regulatory element of gene expression active in at least some of the root cells of a plant, or (ii) at least a portion of a polynucleotide of any of claims 1 to 13.|(AU2024206960 A1)|Root-specific expression of carbonic anhydrase increases the environmental carbon sequestration ability of plants. Here, a plant is genetically engineered so that its heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment. These genetically altered plants demonstrate increased levels of carbonic anhydrase activity in the extracellular environment of the plant roots, which enhances carbon sequestration in extracellular environments such as soil.|(IN202517071665 A)|Root-specific expression of carbonic anhydrase increases the environmental carbon sequestration ability of plants. Here, a plant is genetically engineered so that its heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment. These genetically altered plants demonstrate increased levels of carbonic anhydrase activity in the extracellular environment of the plant roots, which enhances carbon sequestration in extracellular environments such as soil.|(EP4649146 A1)|Root-specific expression of carbonic anhydrase increases the environmental carbon sequestration ability of plants. Here, a plant is genetically engineered so that its heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment. These genetically altered plants demonstrate increased levels of carbonic anhydrase activity in the extracellular environment of the plant roots, which enhances carbon sequestration in extracellular environments such as soil.|(JP2026504057 A)| The root-specific expression of carbonic anhydrase increases the environmental carbon-isolating ability of plants. The plant is genetically engineered so that the plant's inherited genetic material contains a gene encoding a carbonic anhydrase protein that can be transported under the control of a promoter active in the root cell so that carbonic anhydrase is transported from the plant root into the extracellular environment. These genetically modified plants demonstrate an increase in the level of carbonic anhydrase activity in the extracellular environment of plant roots, enhancing carbon sequestration in the extracellular environment, for example, soil.|IPC codes|(JP2026504057 A)|A01H-005/06|A01H-005/10|A01H-006/06|A01H-006/20|A01H-006/38|A01H-006/46|A01H-006/54|A01H-006/60|A01H-006/82|A01H-007/00|Title|(WO2024149976 A1)|Carbon sequestration with transgenic plants expressing carbonic anhydrase|(AR-131571 A1)|Removal of atmospheric carbon dioxide using a biomodification-enhanced weathering mechanism|(AU2024206960 A1)|Carbon sequestration with transgenic plants expressing carbonic anhydrase|(BR112025014035 A0)|Carbon sequestration with transgenic plants expressing carbonic anhydrase|(BR112025014035 A2)|Carbon sequestration with transgenic plants that express carbon anhydrase|(IN202517071665 A)|Carbon sequestration with transgenic plants expressing carbonic anhydrase|(CA3279193 A1)|Carbon sequestration with transgenic plants expressing carbonic anhydrase|(EP4649146 A1)|Carbon sequestration with transgenic plants expressing carbonic anhydrase|(JP2026504057 A)|Carbon sequestration in transgenic plants expressing carbonic anhydrase| Biotechnology|Food chemistry C12N-009/22|C12N-009/88|C12N-015/82/59|C12Y-402/01001 C12N-009/22|C12N-009/88|C12N-015/82/59|C12Y-402/01001 A01H-005/06|A01H-005/10|A01H-006/06|A01H-006/20|A01H-006/38|A01H-006/46|A01H-006/54|A01H-006/60|A01H-006/82|A01H-007/00|C12N-001/21|C12N-005/10|C12N-009/14|C12N-009/22|C12N-009/88|C12N-015/09|C12N-015/29|C12N-015/55|C12N-015/63|C12N-015/82 A01H-005/06|A01H-005/10|A01H-006/06|A01H-006/20|A01H-006/38|A01H-006/46|A01H-006/54|A01H-006/60|A01H-006/82|A01H-007/00|C12N-001/21|C12N-005/10|C12N-009/14|C12N-009/22|C12N-009/88|C12N-015/09|C12N-015/29|C12N-015/55|C12N-015/63|C12N-015/82 US4151310|WO202287289|WO200122806|WO2015183935|WO2013159228 US4151310 42394485 WHO=Examiner SELF=N CAT=X|WO202287289 107406107 WHO=Examiner SELF=N CAT=A|WO200122806 1260195 WHO=Examiner SELF=N CAT=A|WO2015183935 71547118 WHO=Applicant SELF=N|WO2013159228 46323365 WHO=Applicant SELF=N 国際公開第2015/183935号|国際公開第2013/159228号 |US4151310; XP055683182; XP093145281; WO202287289; XP093145296; WO200122806; WO2015183935; WO2013159228; XP002132452; XP019727662; XP002127064||||||| |(WO2024/149976)|International Search Report [Examiner]|-A. PAL ET AL: "Transgenic overexpression of Leucaena [beta]-carbonic anhydrases in tobacco does not affect carbon assimilation and overall biomass", PLANT BIOSYSTEMS - AN INTERNATIONAL JOURNAL DEALING WITH ALL ASPECTS OF PLANT BIOLOGY, vol. 150, no. 5, 8 January 2015 (2015-01-08), pages 932 - 941, XP055683182, ISSN: 1126-3504, DOI: 10.1080/11263504.2014.993739|-BORISJUK NIKOLAI V. ET AL: "Production of recombinant proteins in plant root exudates", NATURE BIOTECHNOLOGY, vol. 17, no. 5, 1 May 1999 (1999-05-01), New York, pages 466 - 469, XP093145281, ISSN: 1087-0156, DOI: 10.1038/8643|-ZAIDI SANIYA ET AL: "Microbial carbonic anhydrase mediated carbon capture, sequestration &amp; utilization: A sustainable approach to delivering bio-renewables", BIORESOURCE TECHNOLOGY, vol. 365, 22 October 2022 (2022-10-22), AMSTERDAM, NL, pages 128174, XP093145296, ISSN: 0960-8524, DOI: 10.1016/j.biortech.2022.128174|-BOONE, C. D.GILL, S.HABIBZADEGAN, A.MCKENNA, R.: "Carbonic anhydrase: An efficient enzyme with possible global implications", INTERNATIONAL JOURNAL OF CHEMICAL ENGINEERING, 2013, Retrieved from the Internet &lt;URL:https://doi.org/10.1155/2013/813931&gt;|-CHEN, L., CAI, Y., LIU, X., GUO, C., SUN, S., WU, C., JIANG, B., HAN, T., &amp; HOU, W.: "Soybean hairy roots produced in vitro by Agrobacterium rhizogenes-mediated transformation", THE CROP JOURNAL, vol. 6, no. 2, 2018, pages 162 - 171, Retrieved from the Internet &lt;URL:https://doi.org/10.1016/j.cj.2017.08.006&gt;|-CLOUGH S.BENT A: "Floral dip: a simplified method for Agrobacterium-mediated transformation of Arabidopsis thaliana", PLANT J, vol. 16, no. 6, 1998, pages 735 - 743, XP002132452, DOI: 10.1046/j.1365-313x.1998.00343.x|-DIMARIO, R. J., CLAYTON, H., MUKHERJEE, A., LUDWIG, M., &amp; MORONEY, J. V.: "Plant Carbonic Anhydrases: Structures, Locations, Evolution, and Physiological Roles", MOLECULAR PLANT, vol. 10, no. 1, 2017, pages 30 - 46, Retrieved from the Internet &lt;URL:https://doi.org/10.1016/j.molp.2016.09.001&gt;|-HAYASHI, T., SHIMODA, Y., SATO, S., TABATA, S., IMAIZUMI-ANRAKU, H., &amp; HAYASHI, M.: "Rhizobial infection does not require cortical expression of upstream common symbiosis genes responsible for the induction of Ca2+ spiking", JOURNAL, vol. 77, no. 1, 2014, pages 146 - 159, Retrieved from the Internet &lt;URL:https://doi.org/10.1111/tpj.12374&gt;|-HATA, N., FUTAMURA, H.: "PRODUCTION OF SOYBEAN PLANTS FOR HYDROPONIC CULTIVATION FROM SEEDLING CUTTINGS IN A MEDIUM CONTAINING RHIZOBIUM INOCULUM DEPENDING ON VARIOUS CONCENTRATIONS OF NUTRIENT SOLUTION AND DIFFERENT NITROGEN SOURCES", JOURNAL OF HORTICULTURAL RESEARCH, vol. 28, no. 2, pages 71 - 82|-HIRAKAWA, Y.SENDA, M.FUKUDA, K.YU, H. Y.ISHIDA, M.TAIRA, M.KINBARA, K.SENDA, T.: "Characterization of a novel type of carbonic anhydrase that acts without metal cofactors", BMC BIOLOGY, vol. 19, no. 1, 2021, Retrieved from the Internet &lt;URL:https://doi.org/10.1186/s12915-021-01039-8&gt;|-HOROWITZ, C. A.: "Paris Agreement", INTERNATIONAL LEGAL MATERIALS, vol. 55, no. 4, 2016, pages 740 - 755, Retrieved from the Internet &lt;URL:https://doi.org/10.1017/S0020782900004253&gt;|-LI, G.YANG, S.LI, M.QIAO, Y.&amp; WANG, J.: "Functional analysis of an Aspergillus ficuum phytase gene in Saccharomyces cerevisiae and its root-specific, secretory expression in transgenic soybean plants", BIOTECHNOLOGY LETTERS, vol. 31, no. 8, 2009, pages 1297 - 1303, XP019727662, Retrieved from the Internet &lt;URL:https://doi.org/10.1007/s10529-009-9992-6&gt; DOI: 10.1007/s10529-009-9992-6|-LI, Y.LIU, X.CHEN, R.TIAN, J.FAN, Y.ZHOU, X.: "Genome-scale mining of root-preferential genes from maize and characterization of their promoter activity", BMC PLANT BIOLOGY, vol. 19, no. 1, 2019, Retrieved from the Internet &lt;URL:https://doi.org/10.1186/s12870-019-2198-8&gt;|-MARQUES-BUENO, M. M.MORAO, A. K.CAYREL, A.PLATRE, M. P.BARBERON, M.CAILLIEUX, E.COLOT, V.JAILLAIS, Y.ROUDIER, F.VERT, G.: "A versatile Multisite Gateway-compatible promoter and transgenic line collection for cell type-specific functional genomics in Arabidopsis", PLANT JOURNAL, vol. 85, no. 2, 2016, pages 320 - 333, Retrieved from the Internet &lt;URL:https://doi.org/10.1111/tpj.13099&gt;|-MASSON-DELMOTTE, V. , P. Z. H.-O. P. D. R. J. S. P. R. S. A. P. W. M.-O. C. P. R. P.S. C. J. B. R. M. Y. C. X. Z. M. I. G. E. L. T: "In Global Warming of 1.5°C. An IPCC special report.", 2018, CAMBRIDGE UNIVERSITY PRESS, article "IPCC, 2018: Summary for Policymakers", pages: 3 - 24|-MATT, A.-S.CHANG, W. W.HU, M. Y.: "Extracellular carbonic anhydrase activity promotes a carbon concentration mechanism in metazoan calcifying cells", PROCEEDINGS OF THE NATIONAL ACADEMY OF SCIENCES, vol. 119, no. 40, 2022|-OZDEMIR, E.: "Biomimetic CO2 Sequestration: 1. Immobilization of Carbonic Anhydrase within Polyurethane Foam", ENERGY FUELS, vol. 23, 7 August 2009 (2009-08-07), pages 5725 - 5730|-STEGER, F.REICH, J.FUCHS, W.RITTMANN, S. K. M. R.GUBITZ, G. M.RIBITSCH, D.BOCHMANN, G.: "Comparison of Carbonic Anhydrases for CO2 Sequestration", INTERNATIONAL JOURNAL OF MOLECULAR SCIENCES, vol. 23, no. 2, 2022, Retrieved from the Internet &lt;URL:https://doi.org/10.3390/ijms23020957&gt;|-STREFLER, J.AMANN, T.BAUER, N.KRIEGLER, E.HARTMANN, J.: "Potential and costs of carbon dioxide removal by enhanced weathering of rocks", ENVIRONMENTAL RESEARCH LETTERS, vol. 13, no. 3, 2018, Retrieved from the Internet &lt;URL:https://doi.org/10.1088/1748-9326/aaa9c4&gt;|-SULTANA, S. M., FRAZIER, T. P., MILLWOOD, R. J., LENAGHAN, S. C., &amp; STEWART JR, N. C.: "Development and validation of a novel and robust cell culture system in soybean (Glycine max (L.) Merr.) for promoter screening", PLANT CELL REPORTS, vol. 38, 2019, pages 1329 - 1345|-VERDAGUER B.DE KOCHKO A.BEACHY R. N.FAUQUET C.: "Isolation and expression in transgenic tobacco and rice plants, of the cassava vein mosaic virus (CVMV) promoter", PLANT MOL BIOL, vol. 31, no. 6, 1996, pages 1129 - 39, XP002127064, DOI: 10.1007/BF00040830|||||||| PENDING (EP4649146)|PENDING|(WO2024/149976)|PENDING|(JP2026504057)|PENDING|(CN120548358)|PENDING|(BR112025014035)|PENDING|(IN202517071665)|PENDING|(AU2024206960)|PENDING|(AR131571)|PENDING|(CA3279193)|PENDING ALIVE (EP4649146)|ALIVE|(WO2024/149976)|ALIVE|(JP2026504057)|ALIVE|(CN120548358)|ALIVE|(BR112025014035)|ALIVE|(IN202517071665)|ALIVE|(AU2024206960)|ALIVE|(AR131571)|ALIVE|(CA3279193)|ALIVE (EP4649146)|LEGAL DETAILS FOR EP4649146|Actual or expected expiration date=2044-01-05|Legal state=ALIVE|Status=PENDING|Event publication date=2024-01-05|Event code=EP/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=EP EP24700478|Application date=2024-01-05|Standardized application number=2024EP-0700478|Event publication 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number=AR131571|Publication stage code=A1|Publication date=2025-04-09|Standardized publication number=AR-131571|(CA3279193)|LEGAL DETAILS FOR CA3279193|Actual or expected expiration date=2044-01-05|Legal state=ALIVE|Status=PENDING|Event publication date=2024-01-05|Event code=CA/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CA CA3279193|Application date=2024-01-05|Standardized application number=2024CA-3279193|Event publication date=2024-07-18|Event code=CA/A1|Event group=Examination events|Application laid open|Publication country=CA|Publication number=CA3279193|Publication stage code=A1|Publication date=2024-07-18|Standardized publication number=CA3279193 (EP4649146)|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR|(EP4649146)|Extension States: BA|(EP4649146)|Validation States: MA, MD, TN, KH|(WO2024/149976)|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW|(WO2024/149976)|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ|(WO2024/149976)|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR|(WO2024/149976)|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML|(WO2024/149976)|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (EP4649146)|EP|(WO2024/149976)|WO; AU; BR; CA; CN; EP; IN; JP|(JP2026504057)|JP|(CN120548358)|CN|(BR112025014035)|BR|(IN202517071665)|IN|(AU2024206960)|AU|(AR131571)|AR|(CA3279193)|CA https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=iCBy9VOVqJVtLeCnpQITGqCa4vFyxJplNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006539651&ekey=2310&xpn=EP4649146&kind=A1 https://register.epo.org/application?number=EP24700478 https://permalink.orbit.com/RenderStaticFirstPage?XPN=jm3DaHO%252BV2DWqxLm4QBXD3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT GB (WO2024/149976)|GB (WO2024/149976)|NAME=WILD BIOSCIENCE LTD 115k Olympic Avenue Milton Park Abingdon Oxfordshire OX14 4SA , COUNTRY=GB (EP4649146)|GB|(WO2024/149976)|GB|||(AU2024206960)|AU|(CA3279193)|CA (EP4649146)|NAME=Impact Intellectual Property LLP 1 Sans Walk , CITY=London EC1R 0LT , COUNTRY=GB , REG=101929181|(WO2024/149976)|NAME=ICELY, Dominic Impact Intellectual Property LLP 1 Sans Walk London Greater London EC1R 0LT , POSTCODE=EC1R 0LT , COUNTRY=GB|(JP2026504057)|NAME=MURAYAMA YASUHIKO , REG=100108453NAME=IIDA MASAHITO , REG=100188558NAME=JITSUHIRO SHINYA , REG=100110364|(CN120548358)|NAME=CHENG MIAO;CHENG & PENG INTELLECTUAL PROPERTY LAW OFFICE , REG=11436NAME=TANG LI;CHENG & PENG INTELLECTUAL PROPERTY LAW OFFICE , REG=11436|(AU2024206960)|NAME=Spruson & Ferguson GPO Box 3898 , CITY=Sydney , STATE=NSW , POSTCODE=2001 , COUNTRY=AU|(CA3279193)|NAME=SMART & BIGGAR LP Scotia Plaza, 40 King Street West 40th Floor , CITY=Toronto , POSTCODE=M5H 3Y2 , COUNTRY=CA , REG=9975a484-2887-4ac6-98ad-669ac5f8e9dd (EP4649146)|GB; GB; GB|(WO2024/149976)|GB; GB; GB|||||||(CA3279193)|GB; GB; GB (EP4649146)|NAME=HENDRON, Ross, CITY=Abingdon Oxfordshire OX14 4SA, COUNTRY=GB |NAME=KELLY, Steven, CITY=Abingdon Oxfordshire OX14 4SA, COUNTRY=GB |NAME=COSTELLO, Rona, CITY=Abingdon Oxfordshire OX14 4SA, COUNTRY=GB|(WO2024/149976)|NAME=HENDRON, Ross c/o Wild Bioscience Ltd 115k Olympic Avenue Milton Park Abingdon Oxfordshire OX14 4SA, POSTCODE=OX14 4SA, COUNTRY=GB |NAME=KELLY, Steven c/o Wild Bioscience Ltd 115k Olympic Avenue Milton Park Abingdon Oxfordshire OX14 4SA, POSTCODE=OX14 4SA, COUNTRY=GB |NAME=COSTELLO, Rona c/o Wild Bioscience Ltd 115k Olympic Avenue Milton Park Abingdon Oxfordshire OX14 4SA, POSTCODE=OX14 4SA, COUNTRY=GB|(JP2026504057)|NAME=Ross Hendron|NAME=Stephen Kelly|NAME=Rona Costello|(CN120548358)|NAME=HUNTON RUSS|NAME=KELLY STEPHEN|NAME=COSTELLO ROBERT|(BR112025014035)|NAME=HENDRON ROSS|NAME=KELLY STEVEN|NAME=COSTELLO RONA|(IN202517071665)|NAME=Hendron Ross|NAME=Kelly Steven|NAME=Costello Rona|(AU2024206960)|NAME=HENDRON, Ross|NAME=KELLY, Steven|NAME=COSTELLO, Rona|(AR131571)|NAME=COSTELLO, RONA|NAME=HENDRON, ROSS|NAME=KELLY, STEVEN|(CA3279193)|NAME=HENDRON Ross c/o Wild Bioscience Ltd, 115k Olympic Avenue, Milton Park, CITY=Abingdon Oxfordshire, POSTCODE=OX14 4SA, COUNTRY=GB |NAME=KELLY Steven c/o Wild Bioscience Ltd, 115k Olympic Avenue, Milton Park, CITY=Abingdon Oxfordshire, POSTCODE=OX14 4SA, COUNTRY=GB |NAME=COSTELLO Rona c/o Wild Bioscience Ltd, 115k Olympic Avenue, Milton Park, CITY=Abingdon Oxfordshire, POSTCODE=OX14 4SA, COUNTRY=GB 19 9 Titre: (EP4649146)|Carbon sequestration with transgenic plants expressing carbonic anhydrase Résumé: (EP4649146)|Root-specific expression of carbonic anhydrase increases the environmental carbon sequestration ability of plants. Here, a plant is genetically engineered so that its heritable genetic material comprises a gene encoding a transportable carbonic anhydrase protein under the control of a promoter active in root cells, such that the carbonic anhydrase is transported from the roots of the plant into the extracellular environment. These genetically altered plants demonstrate increased levels of carbonic anhydrase activity in the extracellular environment of the plant roots, which enhances carbon sequestration in extracellular environments such as soil. 29 Abstract gpt-4o-mini no The focus is on genetically engineered plants and their ability to sequester carbon, not on the accelerated weathering of minerals or related processes.
27 CN202511396576 CN202511396576 CN121241724 117306247 CN121241724 A 2026-01-02 [CN121241724] 2025-09-28 2025-09-28 2026-01-02 (CN121241724)|2045-09-28 (CN121241724)|Carbon sequestration and emission reduction process with straw as raw material in acidic soil scene (CN121241724)|The invention discloses a carbon sequestration and emission reduction process taking straw as a raw material in an acid soil scene, which comprises the following steps: collecting straw, removing impurities from the straw, crushing and cutting the straw, degrading the straw, applying a modifier on the surface of the crushed straw, performing high-temperature pyrolysis treatment on the straw to form biochar, and applying the biochar. Halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposition bacteria are prepared and mixed to form a biochar fungicide complex, the biochar fungicide complex is fixed in pores of biochar according to the proportion of 1: 2, and then the biochar is added into the acid soil; according to the method, straw is collected, subjected to impurity removal treatment and then subjected to smashing and cutting treatment, a three-layer stubble burying structure constructed through combined operation of a hydraulic turnover plow and a rotary cultivator is matched with a humic acid binder to form a honeycomb-shaped pore structure, and the air permeability, the water retention property and the fertilizer retention property of soil can be enhanced; and the red mud solidification layer can also prevent bottom layer leakage. GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES INSTITUTE OF AGRICULTURAL RESOURCES & ENVIRONMENT (CN121241724)|GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES, INSTITUTE OF AGRICULTURAL RESOURCES AND ENVIRONMENT ([CN]) HUANG QIAOYI|TANG SHUANHU|HUANG JIANFENG|HUANG XU|WU TENGFEI|ZHANG MU|PANG YUWAN|YI QIONG|DING WUHAN|WU YONGPEI|CENG KE|LI PING|FU HONGTING|LUO HAIBIN (CN121241724)|HUANG QIAOYI|TANG SHUANHU|HUANG JIANFENG|HUANG XU|WU TENGFEI|ZHANG MU|PANG YUWAN|YI QIONG|DING WUHAN|WU YONGPEI|CENG KE|LI PING|FU HONGTING|LUO HAIBIN (CN121241724)|SUN YONG;BEIJING SHENGGUANGXINHE IP FIRM|Reg. Nb: 16117 (CN121241724)|Hundreds of millions of tons of straws are discarded or burned by farmers every year in the world, the burning of the straws not only causes atmospheric pollution, but also increases the emission of greenhouse gases, further aggravates the influence of climate change, and simultaneously, the stacking or burying of the straws can cause the emission of harmful gases such as methane, thereby causing a larger environmental burden, the straws are one of wastes generated in a large amount in agricultural production, and hundreds of millions of tons of straws are discarded or burned by the farmers every year in the world. The burning of the straw not only causes atmospheric pollution, but also increases the emission of greenhouse gases, further aggravates the influence of climate change, and stacking or burying of the straw may lead to the emission of harmful gases such as methane, causing a larger environmental burden, in the aspect of soil improvement, the traditional method is difficult to effectively improve the soil structure, and simple straw turning and burying cannot form an ideal pore structure, the air permeability, the water retention and the fertilizer retention of the soil cannot be obviously improved, even the soil nutrient balance is possibly influenced slowly due to straw decomposition, the growth and development of crop root systems are not facilitated, and the crop yield and quality are further influenced.| (CN121241724)|1. The carbon fixation and emission reduction process using straw as raw material in acid soil scene is characterized by comprising the following steps of; collecting straws, removing impurities from the straws, and crushing and cutting the straws; Step two, straw degradation treatment, namely, applying an improver to the surface of crushed straw, and performing high-temperature pyrolysis treatment on the straw to form biochar; Step three, applying biochar, preparing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria, mixing to form a biochar microbial inoculum complex, fixing the complex in pores of the biochar according to a volume ratio of 1:2, and adding the biochar into acid soil; fourthly, soil ploughing, constructing a three-layer stubble burying structure in acid soil by adopting the combined operation of a hydraulic tilting plow and a rotary cultivator, and then applying humic acid binder to form a honeycomb pore structure; and fifthly, carbon fixation and emission reduction detection, wherein carbon content detection is carried out once in 1-3 months at the initial stage of applying the straw modified soil, and carbon content changes at different time points are compared to finish carbon fixation and emission reduction. | (CN121241724)|Aiming at the problems, the invention aims to provide a carbon fixation and emission reduction process taking straw as a raw material in an acid soil scene, wherein the carbon fixation and emission reduction process taking straw as the raw material in the acid soil scene is of a three-layer stubble burying structure constructed by combining a hydraulic turnover plow and a rotary cultivator, and is matched with a humic acid binder to form a honeycomb pore structure, so that the air permeability, the water retention property and the fertilizer retention property of soil can be enhanced, the red mud solidified layer can also prevent the leakage of a bottom layer, the physicochemical property of the soil is optimized, an excellent environment is created for the growth of crops, the porous property in straw fibers is favorable for adsorbing and retaining the nutrients, and the nutrient loss is reduced.The invention aims at realizing the technical scheme that the carbon fixation and emission reduction process taking straw as raw material in acid soil scene comprises the following steps of;|The invention discloses a carbon fixation and emission reduction process taking straws as raw materials in an acid soil scene, which comprises the steps of collecting the straws, removing impurities from the straws, crushing and cutting the straws, degrading the straws, applying an improver on the surfaces of the crushed straws, performing high-temperature pyrolysis treatment on the straws to form biochar, applying the biochar, preparing halophilic methane-oxidizing bacteria and high-temperature cellulose-decomposing bacteria, mixing to form a biochar microbial inoculum complex, fixing the complex in pores of the biochar according to a ratio of 1:2, and adding the biochar into the acid soil.|The invention relates to the technical field of carbon sequestration and emission reduction, in particular to a carbon sequestration and emission reduction process using straw as a raw material in an acid soil scene.| (CN121241724)|STRAW(100,58)|EMISSION REDUCTION(100,23)|ACID SOIL SCENE(100,19)|RAW MATERIAL(100,19)|CARBON FIXATION(100,14)|BIOCHAR MICROBIAL INOCULUM COMPLEX(100,4)|STRAW TON(89,2)|BIOCHAR PORE(71,4)|SOIL FERTILIZER RETENTION(67,1)|CRUSHED STRAW(64,4)|FERTILIZER RETENTION(58,3)|HALOPHILIC METHANE OXIDIZING BACTERIUM(54,8)|HYDRAULIC TURNOVER PLOW(53,2)|HYDRAULIC TILTING PLOW(51,3)|STRAW DECOMPOSITION(46,1)|PYROLYSIS TREATMENT(45,4)|CARBON SEQUESTRATION(44,12)|INOCULUM COMPLEX(44,4)|REMOVING IMPURITY(41,4)|SOIL PHYSICOCHEMICAL PROPERTY(41,1)|SOIL PLOWING(39,3)|COLLECTING STRAW(37,3)|STRAW TURNING(37,1)|BIOCHAR(36,17)|HUMIC ACID BINDER(36,13)|BIOCHAR BACTERIAL AGENT COMPLEX(36,4)|STRAW DEGRADATION TREATMENT(36,3)|SOIL NUTRIENT BALANCE(36,1)|STRAW MODIFIED SOIL(34,3)|FARMER(32,2)|NOXIOUS GAS(31,3)|LARGE ENVIRONMENTAL BURDEN(30,2)|IMPROVER(29,6)|CRUSHING(29,4)|ATMOSPHERIC POLLUTION(29,2)|STACK(29,2)|CRUSHED STRAW SURFACE(28,4)|RED MUD LAYER SOLIDIFICATION(28,2)|STRAW FIBER(28,2)|HONEYCOMB PORE STRUCTURE(27,5)|APPLYING BIOCHAR(26,3)|CARBON CONTENT DETECTION(26,1)|MODIFIER(25,16)|METHANE OXIDIZING BACTERIUM(25,8)|BACTERIA(25,7)|STRAW COMPOSITE LAYER(25,6)|ROTARY CULTIVATOR(25,5)|RESISTANT CELLULOSE(25,4)|NUTRIENT LOSS(25,2)|SOIL ORGANIC COMPOSITE(22,2)|CRUSHING TREATMENT(21,3)|PHYSICOCHEMICAL PROPERTY(21,1)|METHANE(20,4)|GREENHOUSE GAS(20,2)|MINERAL MAGNESIUM(18,3)|RED MUD(17,8)|PORE DISTRIBUTION(17,3)|EMISSION REDUCTION DETECTION(17,2)|ACID SOIL(16,10)|NUTRIENT(16,4)|PORE STRUCTURE(16,1)|EMISSION REDUCTION(15,5)|CROP YIELD(15,1)|STRAW MULTISTAGE CRUSHING PRETREATMENT(15,1)|GROUND(14,26)|BIOCHAR MIXED LAYER(14,4)|AIR PERMEABILITY(14,3)|STRAW DRY WEIGHT(14,3)|BOTTOM LAYER LEAKAGE(14,1)|SOIL IMPROVEMENT(14,1)|GAS ANALYZER(13,4)|CARBON CONTENT(13,3)|FULL COMBUSTION(13,3)|INOCULANT(13,3)|WATER RETENTION(13,3)|TEMPERATURE FURNACE(13,2)|CLIMATE CHANGE(12,4)|DRY ENVIRONMENT(12,3)|HONEYCOMB SHAPED VOID(12,3)|LIGHT IMPURITY(12,3)|MIXED ATMOSPHERE(12,3)|SOIL SAMPLE(11,8)|THREE STAGE GRADIENT PYROLYSIS(11,5)|AGRICULTURAL PRODUCTION(11,2)|CROP ROOT SYSTEM(11,1)|THREE LAYER STUBBLE(10,6)|FIBER CRACKING DEGREE(10,3)|VOLUME RATIO(9,10)|SAMPLING(9,3)|STANDING(9,3)|STRAW SECTION(9,3)|ACIDITY NEUTRALIZATION(9,2)|SOIL PARTICLE(8,4)|FAN(8,3)|NITROGEN SOURCE(8,3)|MAGNESIUM INORGANIC SUBSTANCE(8,2)|PLANT RESIDUE(7,4)|BOTTOM LAYER(7,2)|SOIL STRUCTURE(7,1)|HIGH TEMPERATURE PYROLYSIS TREATMENT(6,4)|HYDROCHLORIC ACID(6,3)|CHARCOAL BACTERIAL AGENT COMPLEX(6,2)|STRAW POWDER(6,2)|FERTILIZATION STRATEGY(6,1)|MICROORGANISM EMISSION(6,1)|STRAW PURITY(6,1)|THINNED STRAW(6,1)|SURVIVAL RATE(5,3)|ADSORPTIVITY(5,2)|ECOLOGICAL ENVIRONMENTAL POLLUTION(5,1)|STRAW CUTTING(5,1)|TRADITIONAL METHOD(5,1)|ORGANIC ACID(4,3)|COHESION(4,2)|CONTENT DETECTION(4,2)|NUTRIENT AVAILABILITY(4,2)|THALLUS SIZE(4,2)|ANAEROBIC ENVIRONMENT(4,1)|METHANE GENERATION(4,1)|STABLE BIOCHAR(4,1)|STEP THREE(3,3)|CARBON PERMEABLE SOIL(3,1)|CELL SIZE(3,1)|EQUIPMENT ABRASION(3,1)| (CN121241724)|1. The carbon fixation and emission reduction process using straw as raw material in acid soil scene is characterized by comprising the following steps of;| collecting straws, removing impurities from the straws, and crushing and cutting the straws; | Step two, straw degradation treatment, namely, applying an improver to the surface of crushed straw, and performing high-temperature pyrolysis treatment on the straw to form biochar; | Step three, applying biochar, preparing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria, mixing to form a biochar microbial inoculum complex, fixing the complex in pores of the biochar according to a volume ratio of 1:2, and adding the biochar into acid soil; | fourthly, soil ploughing, constructing a three-layer stubble burying structure in acid soil by adopting the combined operation of a hydraulic tilting plow and a rotary cultivator, and then applying humic acid binder to form a honeycomb pore structure; | and fifthly, carbon fixation and emission reduction detection, wherein carbon content detection is carried out once in 1-3 months at the initial stage of applying the straw modified soil, and carbon content changes at different time points are compared to finish carbon fixation and emission reduction. |2. The carbon sequestration and emission reduction process using straw as raw material in acid soil scene according to claim 1, wherein in the first step, lighter impurities are removed by a fan, the straw is separated from soil and stone by a screen, the impurities are separated, the straw is crushed, the straw is longitudinally cut into 5-8cm straw sections, and the transverse crushing treatment leads the fiber cracking degree to be more than or equal to 85% and the crushing uniformity variation coefficient to be less than or equal to 10%.|3. The carbon sequestration and emission reduction process using straw as raw material in acid soil scene according to claim 1, wherein in the second step, the obtained straw is mixed with modifier according to the mixing amount of 5-8wt%, and three-stage gradient pyrolysis is carried out under mixed atmosphere with volume ratio of CO 2 and N 2 of 1:3.|4. The carbon sequestration and emission reduction process using straw as raw material in the acid soil scene of claim 1, wherein in the third step, the survival rate of the biochar bacterial agent complex is not less than 90%/30 days, and the biochar bacterial agent complex is applied according to 20-30% of dry weight of straw.|5. The carbon sequestration and emission reduction process using straw as raw material in acid soil scene according to claim 1, wherein in the fourth step, one layer is a biochar mixed layer, two layers are straw composite layers, three layers are red mud solidified layers, the biochar mixed layer is 0-10cm deep, the straw composite layers are 10-25cm deep, the red mud solidified layers are 25-40cm deep, and then the honeycomb-shaped void structure of the soil organic composite body is formed by adding humic acid binder, wherein the humic acid binder is used in an amount of 5t/ha.|6. The carbon sequestration and emission reduction process using straw as raw material in acid soil scene according to claim 1, wherein in the fifth step, soil samples of multiple areas are selected for sampling, the sampling depth is 10-30cm, the soil samples are put into a high temperature furnace, the temperature is 500-600 ℃, full combustion is carried out, organic carbon in the samples is converted into CO 2, and the concentration of CO 2 is measured by a gas analyzer.|7. The carbon sequestration and emission reduction process using straw as raw material in acid soil scene according to claim 1, wherein in the second step, the modifier is modified by hydrochloric acid with concentration of 0.5mol/L, and the solid-liquid volume ratio is 1:5.|8. The carbon sequestration and emission reduction process using straw as raw material in acid soil scene according to claim 3, wherein the three-stage gradient pyrolysis is 200 ℃ per 30min, 400 ℃ per 1h and 550 ℃ per 2h, and the biochar with specific surface area not less than 120m2/g is produced.|9. The carbon sequestration and emission reduction process using straw as raw material in acid soil scene according to claim 1, wherein the modifier is prepared by mixing nitrogen source, inoculant, mineral magnesium and organic acid according to volume ratio of 2:2:5:1, and standing for 2-3d in dry environment to obtain the modifier.|10. The carbon sequestration and emission reduction process using straw as raw material in the acid soil scene of claim 1, wherein the degree of matching between the pore distribution and the cell size in the third step is not less than 90%. (CN121241724)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of carbon sequestration and emission reduction, in particular to a carbon sequestration and emission reduction process using straw as a raw material in an acid soil scene.|BACKGROUND ART|[0002] Straw is one of the wastes produced in large quantities in agricultural production. Hundreds of millions of tons of straws are discarded or burned by farmers every year in the world, the burning of the straws not only causes atmospheric pollution, but also increases the emission of greenhouse gases, further aggravates the influence of climate change, and simultaneously, the stacking or burying of the straws can cause the emission of harmful gases such as methane, thereby causing a larger environmental burden, the straws are one of wastes generated in a large amount in agricultural production, and hundreds of millions of tons of straws are discarded or burned by the farmers every year in the world. The burning of the straw not only causes atmospheric pollution, but also increases the emission of greenhouse gases, further aggravates the influence of climate change, and stacking or burying of the straw may lead to the emission of harmful gases such as methane, causing a larger environmental burden, in the aspect of soil improvement, the traditional method is difficult to effectively improve the soil structure, and simple straw turning and burying cannot form an ideal pore structure, the air permeability, the water retention and the fertilizer retention of the soil cannot be obviously improved, even the soil nutrient balance is possibly influenced slowly due to straw decomposition, the growth and development of crop root systems are not facilitated, and the crop yield and quality are further influenced.|[0003] In the chinese patent CN114471124a, carbon-sulfur emission reduction is performed by setting CO2 and SOX released in a power plant and an industrial production process using fossil or biomass as energy, but the method cannot perform carbon-fixing emission reduction treatment on acid soil and straw, so the invention provides a carbon-fixing emission reduction process using straw as a raw material in an acid soil scene to solve the problems in the prior art.|DISCLOSURE|Disclosure of Invention|[0004] Aiming at the problems, the invention aims to provide a carbon fixation and emission reduction process taking straw as a raw material in an acid soil scene, wherein the carbon fixation and emission reduction process taking straw as the raw material in the acid soil scene is of a three-layer stubble burying structure constructed by combining a hydraulic turnover plow and a rotary cultivator, and is matched with a humic acid binder to form a honeycomb pore structure, so that the air permeability, the water retention property and the fertilizer retention property of soil can be enhanced, the red mud solidified layer can also prevent the leakage of a bottom layer, the physicochemical property of the soil is optimized, an excellent environment is created for the growth of crops, the porous property in straw fibers is favorable for adsorbing and retaining the nutrients, and the nutrient loss is reduced.|[0005] The invention aims at realizing the technical scheme that the carbon fixation and emission reduction process taking straw as raw material in acid soil scene comprises the following steps of;|[0006] collecting straws, removing impurities from the straws, and crushing and cutting the straws; |[0007] Step two, straw degradation treatment, namely, applying an improver to the surface of crushed straw, and performing high-temperature pyrolysis treatment on the straw to form biochar; |[0008] Step three, applying biochar, preparing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria, mixing to form a biochar microbial inoculum complex, fixing the complex in pores of the biochar according to a ratio of 1:2, and adding the biochar into acid soil; |[0009] fourthly, soil ploughing, constructing a three-layer stubble burying structure in acid soil by adopting the combined operation of a hydraulic tilting plow and a rotary cultivator, and then applying humic acid binder to form a honeycomb pore structure; |[0010] And fifthly, carrying out carbon content detection once in 1-3 months at the initial stage of applying the straw modified soil, and comparing carbon content changes at different time points to finish carbon fixation and emission reduction. |[0011] The method is further improved in that in the first step, lighter impurities are removed through a fan, the impurities are separated from soil and stones through a screen, the straws are crushed, the straws are longitudinally cut into 5-8cm straw sections, the transverse crushing treatment is carried out, the fiber cracking degree is more than or equal to 85%, and the crushing uniformity variation coefficient is less than or equal to 10%.|[0012] The improvement is that in the second step, the obtained straw and the modifier are mixed according to the mixing amount of 5-8wt%, and three-stage gradient pyrolysis is carried out under the mixed atmosphere of CO 2 and N 2 with the volume ratio of 1:3.|[0013] The further improvement is that in the third step, the survival rate of the charcoal bacterial agent complex is more than or equal to 90 percent/30 days, and the charcoal bacterial agent complex is applied according to 20-30 percent of the dry weight of the straw.|[0014] The method is further improved in that in the fourth step, the first layer is a biochar mixed layer, the second layer is a straw composite layer, the third layer is a red mud solidified layer, the biochar mixed layer is 0-10cm deep, the straw composite layer is 10-25cm deep, the red mud solidified layer is 25-40cm deep, then a honeycomb-shaped void structure of the soil organic composite body is formed through adding of humic acid binder, and the use amount of the humic acid binder is 5t/ha.|[0015] In the fifth step, soil samples in a plurality of areas are selected for sampling, the sampling depth is 10 cm to 30cm, the soil samples are placed into a high-temperature furnace, the temperature is 500 ℃ to 600 ℃, the full combustion is carried out, organic carbon in the samples is converted into CO 2, and the concentration of CO 2 is measured through a gas analyzer.|[0016] The further improvement is that in the second step, the modifier is modified by hydrochloric acid with the concentration of 0.5mol/L, and the solid-liquid volume ratio is 1:5.|[0017] The further improvement is that the three-stage gradient pyrolysis is carried out at 200 ℃ per 30min, 400 ℃ per 1h and 550 ℃ per 2h, and the biochar with the specific surface area more than or equal to 120m 2/g is produced.|[0018] The further improvement is that the modifier is prepared by mixing a nitrogen source, an inoculant, mineral magnesium and organic acid according to a volume ratio of 2:2:5:1, and standing for 2-3d in a dry environment to obtain the modifier.|[0019] The further improvement is that in the third step, the matching degree of the pore distribution and the thallus size is more than or equal to 90 percent.|[0020] The three-layer stubble burying structure constructed by combining the hydraulic turnover plow and the rotary cultivator has the beneficial effects that the three-layer stubble burying structure is matched with the humic acid binder to form a honeycomb pore structure, the air permeability, the water retention property and the fertilizer retention property of soil can be enhanced, the red mud solidified layer can also prevent the bottom layer from leaking, the physical and chemical properties of the soil are optimized, an excellent environment is created for the growth of crops, the porous property in straw fiber is conducive to adsorbing and retaining the nutrients through the multistage crushing pretreatment of the straw, the nutrient loss is reduced, the biochar can provide a stable nutrient source for the soil, mineral substances and trace elements required by plants are supplied, the biochar is mixed with the halophilic methane-oxidizing bacteria and the high-temperature-resistant cellulose decomposing bacteria in a specific proportion, the straw is converted into the biochar, the emission of harmful gases is avoided, the carbon is stably fixed in the soil, the characteristics of microorganisms and the biochar are fully utilized, the fixed conversion of the straw carbon in the soil is accelerated, the methane generation is inhibited, the carbon emission of the rice field is effectively reduced, and the carbon fixing capacity is improved.|DRAWINGS DESCRIPTION|[0021] In order to more clearly illustrate the embodiments of the invention or the technical solutions of the prior art, the drawings which are used in the description of the embodiments or the prior art will be briefly described, it being obvious that the drawings in the description below are only some embodiments of the invention, and that other drawings can be obtained according to these drawings without inventive faculty for a person skilled in the art.|[0022] FIG. 1 is a flow chart of the steps of the present invention.|INVENTION MODE|Detailed Description|[0023] The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0024] In the description of the present invention, unless explicitly stated and limited otherwise, the terms mounted, connected and coupled are to be construed broadly, and may be, for example, fixedly connected, detachably connected or integrally connected, mechanically connected or electrically connected, directly connected or indirectly connected through intermediaries, or communicating between the two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.|[0025] In the method, CO 2 content in the flue gas can be reduced by more than 96 percent, SO 4 content can be reduced by more than 97 percent, the ultra-low emission standard requirements of China are met, emission reduction of CO 2 and SO 4 is realized, ecological environmental pollution caused by greenhouse effect and sulfur oxide emission is eliminated, but the waste of resources and the environmental pollution are caused by adjusting irrigation and fertilization strategies according to the actual condition of soil, the application further uses the straw crushing pretreatment and the use of an improver to fully utilize the characteristics of the straw crushing pretreatment and the improver to fully utilize the microbial carbon in the soil to form the carbon, and the carbon can be fully utilized to realize the improvement of the water-retaining property of the carbon in the soil, the carbon can be more stable, the carbon-permeable soil can be more stably formed, the soil can be more stably grown, the soil can be more stably and the soil can be more stably formed, and the soil can be more stably and the soil is more air-permeable.|[0026] According to the embodiment shown in fig. 1, the carbon sequestration and emission reduction process using straw as raw material in the acid soil scene is provided, and comprises the following steps of;|[0027] collecting straws, removing impurities from the straws, and crushing and cutting the straws; |[0028] Step two, straw degradation treatment, namely, applying an improver to the surface of crushed straw, and performing high-temperature pyrolysis treatment on the straw to form biochar; |[0029] Step three, applying biochar, preparing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria, mixing to form a biochar microbial inoculum complex, fixing the complex in pores of the biochar according to a ratio of 1:2, and adding the biochar into acid soil; |[0030] fourthly, soil ploughing, constructing a three-layer stubble burying structure in acid soil by adopting the combined operation of a hydraulic tilting plow and a rotary cultivator, and then applying humic acid binder to form a honeycomb pore structure; |[0031] And fifthly, carrying out carbon content detection once in 1-3 months at the initial stage of applying the straw modified soil, and comparing carbon content changes at different time points to finish carbon fixation and emission reduction. |[0032] In the first step, lighter impurities are removed through a fan, the straws, soil and stones are separated through a screen, the straws are crushed, the longitudinal cutting of the straws is carried out to form 5-8cm straw sections, the transverse crushing treatment is carried out to ensure that the fiber cracking degree is more than or equal to 85 percent and the crushing uniformity variation coefficient is less than or equal to 10 percent, the impurities in the straws, including the soil, the stones and the weeds, are removed, the purity of the straws can be improved, the operation efficiency of subsequent treatment equipment can be improved, the equipment abrasion is reduced, and the thinned straws are beneficial to accelerating the composting process and biodegradation and are beneficial to improving the soil fertility.|[0033] In the second step, the obtained straw and the modifier are mixed according to the mixing amount of 5-8wt%, three-stage gradient pyrolysis is carried out under the mixed atmosphere of CO 2 and N 2 with the volume ratio of 1:3, the modifier is applied to promote the straw to form stable biochar in the pyrolysis process, the biochar has a long-term stable carbon structure, the biochar can effectively fix carbon, the emission of carbon dioxide is reduced, the pH value of acid soil is usually lower, and the modifier containing calcium and magnesium mineral substances and straw powder are applied to neutralize the acidity in the soil and improve the pH value of the soil, so that a more favorable environment is provided for plant growth.|[0034] In the third step, the survival rate of the biochar bacterial agent complex is more than or equal to 90 percent/30 days, the biochar bacterial agent complex is prepared according to 20-30 percent of the dry weight of the straw, and the halophilic methane oxidizing bacteria can effectively consume methane in the soil and reduce the emission of the halophilic methane oxidizing bacteria in the atmosphere, so that the influence of climate change is slowed down, the high-temperature resistant cellulose decomposing bacteria can decompose plant residues and the straw, convert the plant residues and the straw into available nutrients, improve the organic matter content of the soil, provide more nutrients for plants and promote the plant growth.|[0035] In the fourth step, the first layer is a biological carbon mixed layer, the second layer is a straw composite layer, the third layer is a red mud solidified layer, the biological carbon mixed layer is 0-10cm deep, the straw composite layer is 10-25cm deep, the red mud solidified layer is 25-40cm deep, the honeycomb-shaped void structure of the soil organic complex is formed by adding humic acid binder, the humic acid binder is 5t/ha, the humic acid binder interacts with minerals, microorganisms and organic matters in the soil, the formation of the honeycomb-shaped void structure is promoted, the humic acid has stronger adsorptivity and cohesiveness, can be combined with soil particles, and the agglomeration structure of the soil particles is improved.|[0036] In the fifth step, soil samples in a plurality of areas are selected for sampling, the sampling depth is 10 cm to 30cm, the soil samples are placed in a high-temperature furnace, the temperature is 500 ℃ to 600 ℃, full combustion is carried out, organic carbon in the samples is converted into CO 2, the concentration of CO 2 is measured through a gas analyzer, the content of organic carbon and inorganic carbon in the soil is measured through a combustion method, accurate carbon content data is provided, and the data is critical to researching the effects of carbon storage, soil health and carbon fixation and emission reduction of the soil.|[0037] In the second step, the modifier is modified by hydrochloric acid with the concentration of 0.5mol/L, and the solid-liquid volume ratio is 1:5.|[0038] Three-stage gradient pyrolysis is carried out at 200 ℃ per 30min, 400 ℃ per 1h and 550 ℃ per 2h, and the biochar with the specific surface area more than or equal to 120m < 2 >/g is produced.|[0039] The modifier is prepared by mixing a nitrogen source, an inoculant, mineral magnesium and organic acid according to a volume ratio of 2:2:5:1, and standing for 2-3d in a dry environment to obtain the modifier.|[0040] In the third step, the matching degree of the pore distribution and the thallus size is more than or equal to 90 percent.|[0041] The carbon fixation and emission reduction process taking straw as raw material in the acid soil scene is characterized in that the straw is heated to a higher temperature of 300-700 ℃ and kept in an anaerobic environment, organic matters of the straw are decomposed into biochar, gas and liquid, then modifier is added, the stable biochar is formed in the pyrolysis process of the straw, the biochar has a long-term stable carbon structure, the biochar can effectively fix carbon, the emission of carbon dioxide is reduced, the acid soil is usually low in pH value, the modifier containing calcium and magnesium mineral substances and straw powder are applied to neutralize the acidity in the soil, the pH value of the soil is improved, microorganisms can effectively consume methane in the soil by adding halophilic methane oxidizing bacteria, the emission of the microorganisms in the atmosphere is reduced, thus slowing down the influence of climate change, if high temperature resistant cellulose decomposing bacteria can decompose plant residues and straws, convert the plant residues and straws into available nutrients, improve the organic matter content of soil, provide more nutrients for plants, promote plant growth, enable humic acid binder to interact with minerals, microorganisms and organic matters in the soil, promote the formation of cellular pore structures, enable humic acid to have stronger adsorptivity and cohesiveness, be combined with soil particles, improve the aggregation structure of the soil particles, finally place a soil sample into a high temperature furnace, fully burn the soil sample at 500-600 ℃, convert organic carbon in the sample into CO 2, and measure the concentration of CO 2 by carrying out carbon fixation and emission reduction detection and a gas analyzer; the organic carbon and inorganic carbon content in the soil is measured by a combustion method, and accurate carbon content data is provided.|[0042] The following table is a table of comparison data of detection before and after carbon fixation and emission reduction.|[0043] |[0044] |[0045] The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof. (CN121241724)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of carbon sequestration and emission reduction, in particular to a carbon sequestration and emission reduction process using straw as a raw material in an acid soil scene.|BACKGROUND ART|[0002] Straw is one of the wastes produced in large quantities in agricultural production. Hundreds of millions of tons of straws are discarded or burned by farmers every year in the world, the burning of the straws not only causes atmospheric pollution, but also increases the emission of greenhouse gases, further aggravates the influence of climate change, and simultaneously, the stacking or burying of the straws can cause the emission of harmful gases such as methane, thereby causing a larger environmental burden, the straws are one of wastes generated in a large amount in agricultural production, and hundreds of millions of tons of straws are discarded or burned by the farmers every year in the world. The burning of the straw not only causes atmospheric pollution, but also increases the emission of greenhouse gases, further aggravates the influence of climate change, and stacking or burying of the straw may lead to the emission of harmful gases such as methane, causing a larger environmental burden, in the aspect of soil improvement, the traditional method is difficult to effectively improve the soil structure, and simple straw turning and burying cannot form an ideal pore structure, the air permeability, the water retention and the fertilizer retention of the soil cannot be obviously improved, even the soil nutrient balance is possibly influenced slowly due to straw decomposition, the growth and development of crop root systems are not facilitated, and the crop yield and quality are further influenced.|[0003] In the chinese patent CN114471124a, carbon-sulfur emission reduction is performed by setting CO2 and SOX released in a power plant and an industrial production process using fossil or biomass as energy, but the method cannot perform carbon-fixing emission reduction treatment on acid soil and straw, so the invention provides a carbon-fixing emission reduction process using straw as a raw material in an acid soil scene to solve the problems in the prior art.|DISCLOSURE|Disclosure of Invention|[0004] Aiming at the problems, the invention aims to provide a carbon fixation and emission reduction process taking straw as a raw material in an acid soil scene, wherein the carbon fixation and emission reduction process taking straw as the raw material in the acid soil scene is of a three-layer stubble burying structure constructed by combining a hydraulic turnover plow and a rotary cultivator, and is matched with a humic acid binder to form a honeycomb pore structure, so that the air permeability, the water retention property and the fertilizer retention property of soil can be enhanced, the red mud solidified layer can also prevent the leakage of a bottom layer, the physicochemical property of the soil is optimized, an excellent environment is created for the growth of crops, the porous property in straw fibers is favorable for adsorbing and retaining the nutrients, and the nutrient loss is reduced.|[0005] The invention aims at realizing the technical scheme that the carbon fixation and emission reduction process taking straw as raw material in acid soil scene comprises the following steps of;|[0006] collecting straws, removing impurities from the straws, and crushing and cutting the straws; |[0007] Step two, straw degradation treatment, namely, applying an improver to the surface of crushed straw, and performing high-temperature pyrolysis treatment on the straw to form biochar; |[0008] Step three, applying biochar, preparing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria, mixing to form a biochar microbial inoculum complex, fixing the complex in pores of the biochar according to a ratio of 1:2, and adding the biochar into acid soil; |[0009] fourthly, soil ploughing, constructing a three-layer stubble burying structure in acid soil by adopting the combined operation of a hydraulic tilting plow and a rotary cultivator, and then applying humic acid binder to form a honeycomb pore structure; |[0010] And fifthly, carrying out carbon content detection once in 1-3 months at the initial stage of applying the straw modified soil, and comparing carbon content changes at different time points to finish carbon fixation and emission reduction. |[0011] The method is further improved in that in the first step, lighter impurities are removed through a fan, the impurities are separated from soil and stones through a screen, the straws are crushed, the straws are longitudinally cut into 5-8cm straw sections, the transverse crushing treatment is carried out, the fiber cracking degree is more than or equal to 85%, and the crushing uniformity variation coefficient is less than or equal to 10%.|[0012] The improvement is that in the second step, the obtained straw and the modifier are mixed according to the mixing amount of 5-8wt%, and three-stage gradient pyrolysis is carried out under the mixed atmosphere of CO 2 and N 2 with the volume ratio of 1:3.|[0013] The further improvement is that in the third step, the survival rate of the charcoal bacterial agent complex is more than or equal to 90 percent/30 days, and the charcoal bacterial agent complex is applied according to 20-30 percent of the dry weight of the straw.|[0014] The method is further improved in that in the fourth step, the first layer is a biochar mixed layer, the second layer is a straw composite layer, the third layer is a red mud solidified layer, the biochar mixed layer is 0-10cm deep, the straw composite layer is 10-25cm deep, the red mud solidified layer is 25-40cm deep, then a honeycomb-shaped void structure of the soil organic composite body is formed through adding of humic acid binder, and the use amount of the humic acid binder is 5t/ha.|[0015] In the fifth step, soil samples in a plurality of areas are selected for sampling, the sampling depth is 10 cm to 30cm, the soil samples are placed into a high-temperature furnace, the temperature is 500 ℃ to 600 ℃, the full combustion is carried out, organic carbon in the samples is converted into CO 2, and the concentration of CO 2 is measured through a gas analyzer.|[0016] The further improvement is that in the second step, the modifier is modified by hydrochloric acid with the concentration of 0.5mol/L, and the solid-liquid volume ratio is 1:5.|[0017] The further improvement is that the three-stage gradient pyrolysis is carried out at 200 ℃ per 30min, 400 ℃ per 1h and 550 ℃ per 2h, and the biochar with the specific surface area more than or equal to 120m 2/g is produced.|[0018] The further improvement is that the modifier is prepared by mixing a nitrogen source, an inoculant, mineral magnesium and organic acid according to a volume ratio of 2:2:5:1, and standing for 2-3d in a dry environment to obtain the modifier.|[0019] The further improvement is that in the third step, the matching degree of the pore distribution and the thallus size is more than or equal to 90 percent.|[0020] The three-layer stubble burying structure constructed by combining the hydraulic turnover plow and the rotary cultivator has the beneficial effects that the three-layer stubble burying structure is matched with the humic acid binder to form a honeycomb pore structure, the air permeability, the water retention property and the fertilizer retention property of soil can be enhanced, the red mud solidified layer can also prevent the bottom layer from leaking, the physical and chemical properties of the soil are optimized, an excellent environment is created for the growth of crops, the porous property in straw fiber is conducive to adsorbing and retaining the nutrients through the multistage crushing pretreatment of the straw, the nutrient loss is reduced, the biochar can provide a stable nutrient source for the soil, mineral substances and trace elements required by plants are supplied, the biochar is mixed with the halophilic methane-oxidizing bacteria and the high-temperature-resistant cellulose decomposing bacteria in a specific proportion, the straw is converted into the biochar, the emission of harmful gases is avoided, the carbon is stably fixed in the soil, the characteristics of microorganisms and the biochar are fully utilized, the fixed conversion of the straw carbon in the soil is accelerated, the methane generation is inhibited, the carbon emission of the rice field is effectively reduced, and the carbon fixing capacity is improved.|DRAWINGS DESCRIPTION|[0021] In order to more clearly illustrate the embodiments of the invention or the technical solutions of the prior art, the drawings which are used in the description of the embodiments or the prior art will be briefly described, it being obvious that the drawings in the description below are only some embodiments of the invention, and that other drawings can be obtained according to these drawings without inventive faculty for a person skilled in the art.|[0022] FIG. 1 is a flow chart of the steps of the present invention.|INVENTION MODE|Detailed Description|[0023] The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0024] In the description of the present invention, unless explicitly stated and limited otherwise, the terms mounted, connected and coupled are to be construed broadly, and may be, for example, fixedly connected, detachably connected or integrally connected, mechanically connected or electrically connected, directly connected or indirectly connected through intermediaries, or communicating between the two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.|[0025] In the method, CO 2 content in the flue gas can be reduced by more than 96 percent, SO 4 content can be reduced by more than 97 percent, the ultra-low emission standard requirements of China are met, emission reduction of CO 2 and SO 4 is realized, ecological environmental pollution caused by greenhouse effect and sulfur oxide emission is eliminated, but the waste of resources and the environmental pollution are caused by adjusting irrigation and fertilization strategies according to the actual condition of soil, the application further uses the straw crushing pretreatment and the use of an improver to fully utilize the characteristics of the straw crushing pretreatment and the improver to fully utilize the microbial carbon in the soil to form the carbon, and the carbon can be fully utilized to realize the improvement of the water-retaining property of the carbon in the soil, the carbon can be more stable, the carbon-permeable soil can be more stably formed, the soil can be more stably grown, the soil can be more stably and the soil can be more stably formed, and the soil can be more stably and the soil is more air-permeable.|[0026] According to the embodiment shown in fig. 1, the carbon sequestration and emission reduction process using straw as raw material in the acid soil scene is provided, and comprises the following steps of;|[0027] collecting straws, removing impurities from the straws, and crushing and cutting the straws; |[0028] Step two, straw degradation treatment, namely, applying an improver to the surface of crushed straw, and performing high-temperature pyrolysis treatment on the straw to form biochar; |[0029] Step three, applying biochar, preparing halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposing bacteria, mixing to form a biochar microbial inoculum complex, fixing the complex in pores of the biochar according to a ratio of 1:2, and adding the biochar into acid soil; |[0030] fourthly, soil ploughing, constructing a three-layer stubble burying structure in acid soil by adopting the combined operation of a hydraulic tilting plow and a rotary cultivator, and then applying humic acid binder to form a honeycomb pore structure; |[0031] And fifthly, carrying out carbon content detection once in 1-3 months at the initial stage of applying the straw modified soil, and comparing carbon content changes at different time points to finish carbon fixation and emission reduction. |[0032] In the first step, lighter impurities are removed through a fan, the straws, soil and stones are separated through a screen, the straws are crushed, the longitudinal cutting of the straws is carried out to form 5-8cm straw sections, the transverse crushing treatment is carried out to ensure that the fiber cracking degree is more than or equal to 85 percent and the crushing uniformity variation coefficient is less than or equal to 10 percent, the impurities in the straws, including the soil, the stones and the weeds, are removed, the purity of the straws can be improved, the operation efficiency of subsequent treatment equipment can be improved, the equipment abrasion is reduced, and the thinned straws are beneficial to accelerating the composting process and biodegradation and are beneficial to improving the soil fertility.|[0033] In the second step, the obtained straw and the modifier are mixed according to the mixing amount of 5-8wt%, three-stage gradient pyrolysis is carried out under the mixed atmosphere of CO 2 and N 2 with the volume ratio of 1:3, the modifier is applied to promote the straw to form stable biochar in the pyrolysis process, the biochar has a long-term stable carbon structure, the biochar can effectively fix carbon, the emission of carbon dioxide is reduced, the pH value of acid soil is usually lower, and the modifier containing calcium and magnesium mineral substances and straw powder are applied to neutralize the acidity in the soil and improve the pH value of the soil, so that a more favorable environment is provided for plant growth.|[0034] In the third step, the survival rate of the biochar bacterial agent complex is more than or equal to 90 percent/30 days, the biochar bacterial agent complex is prepared according to 20-30 percent of the dry weight of the straw, and the halophilic methane oxidizing bacteria can effectively consume methane in the soil and reduce the emission of the halophilic methane oxidizing bacteria in the atmosphere, so that the influence of climate change is slowed down, the high-temperature resistant cellulose decomposing bacteria can decompose plant residues and the straw, convert the plant residues and the straw into available nutrients, improve the organic matter content of the soil, provide more nutrients for plants and promote the plant growth.|[0035] In the fourth step, the first layer is a biological carbon mixed layer, the second layer is a straw composite layer, the third layer is a red mud solidified layer, the biological carbon mixed layer is 0-10cm deep, the straw composite layer is 10-25cm deep, the red mud solidified layer is 25-40cm deep, the honeycomb-shaped void structure of the soil organic complex is formed by adding humic acid binder, the humic acid binder is 5t/ha, the humic acid binder interacts with minerals, microorganisms and organic matters in the soil, the formation of the honeycomb-shaped void structure is promoted, the humic acid has stronger adsorptivity and cohesiveness, can be combined with soil particles, and the agglomeration structure of the soil particles is improved.|[0036] In the fifth step, soil samples in a plurality of areas are selected for sampling, the sampling depth is 10 cm to 30cm, the soil samples are placed in a high-temperature furnace, the temperature is 500 ℃ to 600 ℃, full combustion is carried out, organic carbon in the samples is converted into CO 2, the concentration of CO 2 is measured through a gas analyzer, the content of organic carbon and inorganic carbon in the soil is measured through a combustion method, accurate carbon content data is provided, and the data is critical to researching the effects of carbon storage, soil health and carbon fixation and emission reduction of the soil.|[0037] In the second step, the modifier is modified by hydrochloric acid with the concentration of 0.5mol/L, and the solid-liquid volume ratio is 1:5.|[0038] Three-stage gradient pyrolysis is carried out at 200 ℃ per 30min, 400 ℃ per 1h and 550 ℃ per 2h, and the biochar with the specific surface area more than or equal to 120m < 2 >/g is produced.|[0039] The modifier is prepared by mixing a nitrogen source, an inoculant, mineral magnesium and organic acid according to a volume ratio of 2:2:5:1, and standing for 2-3d in a dry environment to obtain the modifier.|[0040] In the third step, the matching degree of the pore distribution and the thallus size is more than or equal to 90 percent.|[0041] The carbon fixation and emission reduction process taking straw as raw material in the acid soil scene is characterized in that the straw is heated to a higher temperature of 300-700 ℃ and kept in an anaerobic environment, organic matters of the straw are decomposed into biochar, gas and liquid, then modifier is added, the stable biochar is formed in the pyrolysis process of the straw, the biochar has a long-term stable carbon structure, the biochar can effectively fix carbon, the emission of carbon dioxide is reduced, the acid soil is usually low in pH value, the modifier containing calcium and magnesium mineral substances and straw powder are applied to neutralize the acidity in the soil, the pH value of the soil is improved, microorganisms can effectively consume methane in the soil by adding halophilic methane oxidizing bacteria, the emission of the microorganisms in the atmosphere is reduced, thus slowing down the influence of climate change, if high temperature resistant cellulose decomposing bacteria can decompose plant residues and straws, convert the plant residues and straws into available nutrients, improve the organic matter content of soil, provide more nutrients for plants, promote plant growth, enable humic acid binder to interact with minerals, microorganisms and organic matters in the soil, promote the formation of cellular pore structures, enable humic acid to have stronger adsorptivity and cohesiveness, be combined with soil particles, improve the aggregation structure of the soil particles, finally place a soil sample into a high temperature furnace, fully burn the soil sample at 500-600 ℃, convert organic carbon in the sample into CO 2, and measure the concentration of CO 2 by carrying out carbon fixation and emission reduction detection and a gas analyzer; the organic carbon and inorganic carbon content in the soil is measured by a combustion method, and accurate carbon content data is provided.|[0042] The following table is a table of comparison data of detection before and after carbon fixation and emission reduction.|[0043] |[0044] |[0045] The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof. Family Number|(117306247)|117306247|Abstract|(CN121241724 A)|The invention discloses a carbon sequestration and emission reduction process taking straw as a raw material in an acid soil scene , which comprises the following steps : collecting straw , removing impurities from the straw , crushing and cutting the straw , degrading the straw , applying a modifier on the surface of the crushed straw , performing high - temperature pyrolysis treatment on the straw to form biochar , and applying the biochar . Halophilic methane - oxidizing bacteria and high - temperature - resistant cellulose decomposition bacteria are prepared and mixed to form a biochar fungicide complex , the biochar fungicide complex is fixed in pores of biochar according to the proportion of 1 : 2, and then the biochar is added into the acid soil ; according to the method , straw is collected , subjected to impurity removal treatment and then subjected to smashing and cutting treatment , a three - layer stubble burying structure constructed through combined operation of a hydraulic turnover plow and a rotary cultivator is matched with a humic acid binder to form a honeycomb - shaped pore structure , and the air permeability , the water retention property and the fertilizer retention property of soil can be enhanced ; and the red mud solidification layer can also prevent bottom layer leakage . |CPC codes|(CN121241724 A)|A01B - 079/00 |A01B - 079/02 |IPC codes|(CN121241724 A)|A01B - 079/00 |A01B - 079/02 |Title|(CN121241724 A)|Carbon sequestration and emission reduction process with straw as raw material in acidic soil scene | Basic materials chemistry|Other special machines A01B-079/00|A01B-079/02|C09K-017/40|C09K-2101/00|C09K-2109/00 A01B-079/00|A01B-079/02|C09K-017/40|C09K-2101/00|C09K-2109/00 A01B-079/00|A01B-079/02|C09K-017/40|C09K-101/00 A01B-079/00|A01B-079/02|C09K-017/40|C09K-101/00 PENDING (CN121241724)|PENDING ALIVE (CN121241724)|ALIVE (CN121241724)|LEGAL DETAILS FOR CN121241724|Actual or expected expiration date=2045-09-28|Legal state=ALIVE|Status=PENDING|Event publication date=2025-09-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511396576|Application date=2025-09-28|Standardized application number=2025CN-1396576|Event publication date=2026-01-02|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121241724|Publication stage code=A|Publication date=2026-01-02|Standardized publication number=CN121241724|Event publication date=2026-01-02|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2026-01-20|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121241724)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKc+P6QWIJUqIlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080341181&ekey=2173&xpn=CN121241724&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252Fp%252FVYy7oKp3bvC5CngmzoJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121241724)|CN (CN121241724)|NAME=GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES, INSTITUTE OF AGRICULTURAL RESOURCES AND ENVIRONMENT , COUNTRY=CN (CN121241724)|NAME=SUN YONG;BEIJING SHENGGUANGXINHE IP FIRM , REG=16117 (CN121241724)|CN (CN121241724)|NAME=HUANG QIAOYI, COUNTRY=CN |NAME=TANG SHUANHU|NAME=HUANG JIANFENG|NAME=HUANG XU|NAME=WU TENGFEI|NAME=ZHANG MU|NAME=PANG YUWAN|NAME=YI QIONG|NAME=DING WUHAN|NAME=WU YONGPEI|NAME=CENG KE|NAME=LI PING|NAME=FU HONGTING|NAME=LUO HAIBIN 0 1 Titre: (CN121241724)|Carbon sequestration and emission reduction process with straw as raw material in acidic soil scene Résumé: (CN121241724)|The invention discloses a carbon sequestration and emission reduction process taking straw as a raw material in an acid soil scene, which comprises the following steps: collecting straw, removing impurities from the straw, crushing and cutting the straw, degrading the straw, applying a modifier on the surface of the crushed straw, performing high-temperature pyrolysis treatment on the straw to form biochar, and applying the biochar. Halophilic methane-oxidizing bacteria and high-temperature-resistant cellulose decomposition bacteria are prepared and mixed to form a biochar fungicide complex, the biochar fungicide complex is fixed in pores of biochar according to the proportion of 1: 2, and then the biochar is added into the acid soil; according to the method, straw is collected, subjected to impurity removal treatment and then subjected to smashing and cutting treatment, a three-layer stubble burying structure constructed through combined operation of a hydraulic turnover plow and a rotary cultivator is matched with a humic acid binder to form a honeycomb-shaped pore structure, and the air permeability, the water retention property and the fertilizer retention property of soil can be enhanced; and the red mud solidification layer can also prevent bottom layer leakage. 27 Abstract gpt-4o-mini no The article focuses on a carbon sequestration process using straw and biochar in acidic soils, without mention of mineral weathering or CO₂ capture through mineral carbonation.
28 CN202310205812 CN202310205812 CN116177584 105110541 CN116177584 A 2023-05-30 [CN116177584] 2023-03-06 2023-03-06 2023-05-30 (CN116177584)|2025-06-24 (CN116177584)|Method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial byproduct gypsum (CN116177584)|The invention relates to the technical field of resource utilization of industrial by-product gypsum and environmental protection and treatment, and discloses a method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum, which comprises the following steps: 1, introducing ammonia gas into water according to a gas-liquid volume ratio of (700-900): 1, the mixture can be fully dissolved at normal temperature to obtain ammonia water with the concentration of 20%-30%; 2, adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill according to the solid-liquid mass ratio of 1: (2-4), adding a grinding medium, carrying out wet grinding at the temperature of about 20-40 DEG C, introducing 0.4-0.8 MPa CO2 gas to carry out a carbon sequestration reaction, grinding until the pH value is 9, and suspending wet grinding; according to the method for preparing the nano-micron calcium carbonate through wet carbon sequestration of the industrial byproduct gypsum, the byproduct phosphogypsum is fully crushed through the small-particle-size zirconium oxide balls in the wet grinding stage, the contact area of ammonia water and phosphogypsum particles is increased, ion dissolution is improved, CO2 is introduced into a solution for carbon sequestration, and the solid waste carbon sequestration efficiency is improved. HUBEI UNIVERSITY OF TECHNOLOGY (CN116177584)|HUBEI UNIVERSITY OF TECHNOLOGY ([CN]) SU YING|GUANG LUN|HE XINGYANG|YANG JIN|DAI FEI|ZHENG ZHENGQI|BAI SHIYING|WAN ZIHENG (CN116177584)|SU YING|GUANG LUN|HE XINGYANG|YANG JIN|DAI FEI|ZHENG ZHENGQI|BAI SHIYING|WAN ZIHENG (CN116177584)|HUANG DINGJIN;WUHAN SINOPOWER PATENT AGENCY|Reg. Nb: 42237 (CN116177584)|The method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial by-product gypsum has the advantages of low raw material cost, low energy consumption, short time consumption and simple preparation process, and is favorable for industrial production.|compared with common SiC and potassium titanate whiskers in the market, the aragonite calcium carbonate has the advantages of high whiteness, large filling amount and the like, and is relatively low in cost, and the special appearance and the high compatibility with matrix resin during compounding with plastics obviously improve the processing performance and mechanical properties of products, so that the aragonite calcium carbonate is widely applied to the fields of paint coatings, plastics, rubber, printing ink, papermaking, brake pads, frosted materials, daily chemicals, foods, medicines and the like.|the invention provides a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, which comprises the steps of fully crushing shells of larger-particle calcium carbonate through zirconia balls with small particle size during carbon fixation to enable the shells to be continuously exposed out of fresh surfaces, generating calcium carbonate particles with smaller particle size, and simultaneously adding a crystal form regulator AlCl 3 One of the aluminum ions and the ethanol is adhered to the surface of the calcium carbonate to weaken the relative growth speed and reduceThe method has the advantages that the possibility of forming calcite calcium carbonate seed crystals or the solvation of ethanol is adopted to make the system in a low saturation state, create a microenvironment suitable for the formation of aragonite calcium carbonate, and in the continuous impact process, calcium carbonate with smaller particle size is formed to be more favorable for the adsorption of aluminum ions or improve the solvation of ethanol, so that the formation efficiency of aragonite calcium carbonate crystal forms is improved.| (CN116177584)|1. The method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum is characterized by comprising the following steps of:step one: ammonia gas is introduced into water according to the gas-liquid volume ratio of 700-900:1, and ammonia water with the concentration of 20% -30% can be fully dissolved at normal temperature;step two: industrial side for removing impurities from menstruationAdding gypsum and prepared ammonia water into a wet mill according to a solid-liquid mass ratio of 1:2-4, adding a grinding medium, carrying out wet grinding at 20-40 ℃, and simultaneously introducing CO of 0.4-0.8 MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;step three: immediately adding a crystal form regulator after suspending wet grinding, controlling the temperature by a constant temperature controller, and introducing CO 2 The gas is continuously subjected to wet grinding through a grinding medium;step four: wet grinding for 60-90 min, pulping and refining, wet grinding to obtain grain size of 60-1000 nm, sieving the slurry with 100 mesh square sieve to eliminate wet zirconia grinding ball, filtering and drying to obtain aragonite calcium carbonate with purity of 85-95%.| (CN116177584)|Aiming at the defects of the prior art, the invention provides a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, which solves the problem of Ca (OH) in lime milk suspension 2 Low solid content, low production efficiency, relatively high magnesium chloride consumption, high cost and difficult recovery.|The invention relates to the technical fields of resource utilization and environmental protection treatment of industrial by-product gypsum, and discloses a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial by-product gypsum, which comprises the following steps: step one: ammonia gas is introduced into water according to the gas-liquid volume ratio of 700-900:1, and ammonia water with the concentration of 20% -30% can be fully dissolved at normal temperature; step two: taking the industrial byproduct gypsum after impurity removal and prepared ammonia water according to the solid-liquid mass ratio of 1:2Adding the materials into a wet grinder, adding a grinding medium, carrying out wet grinding at about 20-40 ℃, and simultaneously introducing CO at 0.4-0.8 MPa 2 And (3) carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding.|The invention relates to the technical fields of resource utilization and environmental protection treatment of industrial by-product gypsum, in particular to a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial by-product gypsum.| (CN116177584)|CALCIUM CARBONATE(100,61)|CARBON FIXATION(100,39)|BYPRODUCT GYPSUM(100,28)|NANOMICRON CALCIUM CARBONATE(100,25)|NANOMICRON(100,24)|WET CARBON FIXATION(100,13)|MENSTRUATIONADDING GYPSUM(67,1)|ARAGONITE CALCIUM CARBONATE(63,9)|ETHANOL SOLVATION(59,2)|RESOURCE UTILIZATION(57,2)|WET CARBON SEQUESTRATION(50,8)|ZIRCONIA GRINDING BALL(45,2)|ARAGONITE CALCIUM CARBONATE FORMATION(43,2)|ZIRCONIA BALL(39,6)|NANO MICRON CALCIUM CARBONATE(39,4)|POTASSIUM TITANATE WHISKER(38,1)|REMOVING IMPURITY(33,12)|GRINDING MEDIUM(33,11)|ALUMINUM ION(33,2)|GRINDING(32,37)|BYPRODUCT PHOSPHOGYPSUM(32,3)|ENVIRONMENTAL PROTECTION TREATMENT(31,2)|CALCITE CALCIUM CARBONATE(31,1)|INORGANIC MATTER ALCL(28,1)|PAINT COATING(27,1)|MICROENVIRONMENT(26,1)|PHOSPHOGYPSUM PARTICLE(25,3)|LIME MILK SUSPENSION(25,2)|REDUCETHE(25,1)|ENVIRONMENTAL PROTECTION(23,2)|CALCIUM CARBONATE PARTICLE(23,1)|DAILY CHEMICAL(23,1)|SATURATION(23,1)|PLASTIC(22,2)|MATRIX RESIN(22,1)|GRINDING BALL(21,7)|WET GRINDER(21,1)|WET GRINDING(20,7)|WET MILL(20,7)|GROWTH SPEED(20,1)|DIFFICULT RECOVERY(19,1)|SLURRY(18,12)|ION DISSOLUTION(18,3)|CRUSHING(18,1)|PH VALUE(17,11)|PURITY(17,8)|MAGNESIUM CHLORIDE CONSUMPTION(17,2)|PAPERMAKING(17,2)|POTASSIUM TITANATE(17,1)|WHITE(16,3)|SHELL(16,1)|AMMONIA WATER(15,28)|PERFORMING PROCESSING(15,1)|CONSTANT TEMPERATURE CONTROLLER(14,16)|ADSORBENT(14,2)|BRAKE PAD(14,1)|FOOD(14,1)|PRINTING INK(14,1)|SEED CRYSTAL(14,1)|FROSTED MATERIAL(13,1)|SIC(13,1)|AMMONIA GAS(12,18)|LARGE FILLING(12,1)|SPECIAL APPEARANCE(12,1)|GRAIN DIAMETER(11,3)|SOLID CONTENT(11,2)|DESCRIBEDTHE INDUSTRIAL BYPRODUCT GYPSUM(11,1)|ARAGONITE CACO(10,3)|TRAPPING(10,3)|MECHANICAL PROPERTY(10,1)|ROTATING SPEED(9,16)|MAGNESIUM CHLORIDE(9,3)|CRYSTAL FORM REGULATOR ALCL(9,1)|INDUSTRIAL PRODUCTION(8,7)|CURING AGENT(8,2)|STEP FOUR(8,1)|VOLUME RATIO(7,15)|MASS RATIO(7,8)|INORGANIC SUBSTANCE(7,3)|SMALL PARTICLE SIZE(7,3)|LARGE PARTICLE CALCIUM CARBONATE(7,1)|ENERGY CONSUMPTION(6,4)|CALCIUM CARBONATE WHISKER(6,2)|GRAIN SIZE(6,2)|CHEMICAL SOLVENT(6,1)|SEDIMENTATION CLASSIFICATION(6,1)|CRYSTAL ADDITION(5,5)|SOLID WASTE PHOSPHOGYPSUM(5,5)|ZIRCONIA(5,5)|GAS LIQUID VOLUME RATIO(5,4)|MESH SQUARE HOLE(5,4)|CRYSTAL FORM REGULATOR(5,3)|INDUSTRIAL PRODUCTION AMMONIA GAS(5,3)|GREENHOUSE GAS SOLIDIFICATION(5,2)|SOLID LIQUID SEPARATION(5,2)|DAILY PLASTIC INDUSTRY(5,1)|INORGANIC ALCL(5,1)|INVESTIGATION CALCULATION(5,1)|RAW MATERIAL COST(4,2)|CALCIUM CARBONATE ANNUAL DEMAND(4,1)|POLYTYPE CRYSTAL(4,1)|STABLE CALCITE(4,1)|WET MILLINGETHANOL SOLUTION(4,1)| (CN116177584)|1. The method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum is characterized by comprising the following steps of:|step one: ammonia gas is introduced into water according to the gas-liquid volume ratio of 700-900:1, and ammonia water with the concentration of 20% -30% can be fully dissolved at normal temperature;|step two: industrial side for removing impurities from menstruationAdding gypsum and prepared ammonia water into a wet mill according to a solid-liquid mass ratio of 1:2-4, adding a grinding medium, carrying out wet grinding at 20-40 ℃, and simultaneously introducing CO of 0.4-0.8 MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|step three: immediately adding a crystal form regulator after suspending wet grinding, controlling the temperature by a constant temperature controller, and introducing CO 2 The gas is continuously subjected to wet grinding through a grinding medium;|step four: wet grinding for 60-90 min, pulping and refining, wet grinding to obtain grain size of 60-1000 nm, sieving the slurry with 100 mesh square sieve to eliminate wet zirconia grinding ball, filtering and drying to obtain aragonite calcium carbonate with purity of 85-95%.|2. The method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum according to claim 1, wherein the ammonia gas in the first step is industrial production ammonia gas with purity not less than 85%, extremely easy to dissolve in water and ammonia water with concentration of 20% -30% with pH value of 9-10.|3. The method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum according to claim 1, wherein the impurity removal method in the second step is to take a proper amount of by-product gypsum, add chemical solvent, physical adsorbent, chemical curing agent and crystal form regulator to wet grind at the same time, and perform solid-liquid separation and drying after the reaction is completed, thus obtaining the nano-micron calcium carbonate.|4. The method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum according to claim 1, wherein in the second step, the industrial by-product gypsum is mainly phosphogypsum, is solid waste in the wet phosphoric acid process, and mainly comprises CaSO (calcium carbonate) 4 ·2H 2 O, with a 97% ratio, density of 2.5g/cm 3 The grain diameter is 100 μm, the pH value is 4.5, and a small part of impurities are inorganic substances P, F, cd, cu, zn, pb and organic substances C 4 H 8 O 2 S、C 4 H 4 N 2 OS 2 The ratio is 3%.|5. The method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum according to claim 1, wherein the grinding medium in the second and third steps is 0.8mm:0.5mm: zirconia balls with 0.3 mm=1:2:2, the ball-to-material ratio is 7:2-4, and the rotating speed is adjusted to be 200 r/min-800 r/min.|6. The method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum according to claim 1, wherein the introduced CO in the second step 2 CO trapping for purification of industrial process exhaust gas 2 The purity is more than or equal to 45 percent.|7. The method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum according to claim 1, wherein the crystal form control agent in the third step is an inorganic matter AlCl 3 The slurry is added with the concentration controlled between 0.30mol/L and 0.40mol/L, and the temperature is controlled between 60 ℃ and 80 ℃ by a constant temperature controller.|8. The method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum according to claim 1, wherein in the third step, the crystal form control agent is an organic substance, the concentration is 90% ethanol solution, the slurry is added in the volume ratio of 1:1-2 with ammonia water, and the temperature is controlled at 40-60 ℃ by a constant temperature controller.|9. The method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum according to claim 1, wherein the crystal form control agent in the third step is AlCl 3 One of ethanol. (CN116177584)|TECHNICAL FIELD|[0001] The invention relates to the technical fields of resource utilization and environmental protection treatment of industrial by-product gypsum, in particular to a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial by-product gypsum.|BACKGROUND ART|[0002] Phosphogypsum refers to solid waste in the wet phosphoric acid process, and the chemical reaction equation is as follows: ca (Ca) 5 (PO 4 ) 3 X+5H 2 SO 4 +10H 2 O→3H 3 PO 4 +5(CaSO 4 ·2H 2 O) +HX, (wherein X can comprise OH, F, cl or Br), and according to investigation calculation, phosphogypsum is produced by 4 t-6 t per 1t of phosphoric acid production.|[0003] Calcium carbonate belongs to polytype crystal, mainly calcite, aragonite and vaterite are usually present in the most stable calcite form, so that the annual demand of calcium carbonate in China is very large at present, the application fields of calcium carbonate with different morphologies are continuously expanded, the most common morphology of calcium carbonate is spherical, needle-shaped, flaky, chain-locked, cubic, amorphous and the like, aragonite calcium carbonate is taken as an important inorganic product, is a high-performance novel composite material reinforcing and toughening agent, has a complete structure and fewer defects in the interior, can be used in the industries of daily plastics, rubber, papermaking and the like,|[0004] compared with common SiC and potassium titanate whiskers in the market, the aragonite calcium carbonate has the advantages of high whiteness, large filling amount and the like, and is relatively low in cost, and the special appearance and the high compatibility with matrix resin during compounding with plastics obviously improve the processing performance and mechanical properties of products, so that the aragonite calcium carbonate is widely applied to the fields of paint coatings, plastics, rubber, printing ink, papermaking, brake pads, frosted materials, daily chemicals, foods, medicines and the like.|[0005] The Chinese patent CN104790024A has been searched and a method for preparing aragonite type calcium carbonate whisker with high length-diameter ratio is disclosed, which comprises the steps of preparing Ca (OH) with 1.0-8.2wt% 2 Adding magnesium chloride as crystal form regulator into the suspension, introducing CO 2 And N 2 Carbonizing the mixed gas, and finally carrying out suction filtration, washing, drying and crushing to obtain aragonite type calcium carbonate with the length-diameter ratio of 10-26, wherein Ca (OH) is contained in the lime milk suspension by the method 2 The solid content is low, the production efficiency is low, the magnesium chloride consumption is relatively high, the cost is high, and the recovery is difficult.|[0006] Also, it is found that CN1641077 discloses a method for preparing aragonite type calcium carbonate whisker, which comprises preparing slurry from quicklime or slaked lime, using magnesium salt as crystal form control agent, and introducing CO 2 The aragonite calcium carbonate with 93-98% of content is obtained by carbonization, and the magnesium salt solution can be recycled, but the method needs to carry out sedimentation classification on slurry for 3 times, chemical analysis on magnesium salt recovery liquid and the like, has complex operation flow, long reaction time of 4 hours and multiple stages, has the combination rotating speed of 600r/min, and has overlarge energy consumption.|[0007] The literature for preparing the aragonite type calcium carbonate by wet-milling carbon fixation by utilizing the solid waste phosphogypsum is not searched, so the method aims to provide a method for preparing nano-micron calcium carbonate by wet-milling carbon fixation by utilizing industrial byproduct gypsum, and solves the problems of low utilization rate, environmental pollution and the like of the industrial solid waste phosphogypsum while preparing the aragonite type calcium carbonate, changes waste into valuable and solidifies greenhouse gas CO 2 The greenhouse effect is relieved.|DISCLOSURE|Disclosure of Invention|[0008] (one) solving the technical problems|[0009] Aiming at the defects of the prior art, the invention provides a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, which solves the problem of Ca (OH) in lime milk suspension 2 Low solid content, low production efficiency, relatively high magnesium chloride consumption, high cost and difficult recovery.|[0010] (II) technical scheme|[0011] In order to achieve the above purpose, the present invention provides the following technical solutions: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0012] step one: ammonia gas is introduced into water according to the gas-liquid volume ratio of 700-900:1, and ammonia water with the concentration of 20% -30% can be fully dissolved at normal temperature;|[0013] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill according to a solid-liquid mass ratio of 1:2-4, adding a grinding medium, carrying out wet grinding at 20-40 ℃, and simultaneously introducing CO of 0.4-0.8 MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0014] step three: immediately adding a crystal form regulator after suspending wet grinding, controlling the temperature by a constant temperature controller, and introducing CO 2 The gas is continuously subjected to wet grinding through a grinding medium;|[0015] step four: wet grinding for 60-90 min, pulping and refining, wet grinding to obtain grain size of 60-1000 nm, sieving the slurry with 100 mesh square sieve to eliminate wet zirconia grinding ball, filtering and drying to obtain aragonite calcium carbonate with purity of 85-95%.|[0016] Further, the ammonia gas in the first step is industrial production ammonia gas, the purity is more than or equal to 85 percent, the ammonia gas is very easy to be dissolved in water, and the pH value of the ammonia water with the concentration of 20 to 30 percent is 9 to 10.|[0017] And further, the impurity removing method in the second step is to take a proper amount of byproduct gypsum, add a chemical cosolvent, a physical adsorbent, a chemical curing agent and a crystal form regulator to perform wet grinding, and perform solid-liquid separation and drying after the reaction is completed, thus obtaining the gypsum.|[0018] Further, the step two is describedThe industrial byproduct gypsum is mainly phosphogypsum, is solid waste in the wet phosphoric acid process, and mainly comprises CaSO as the component 4 ·2H 2 O, with a 97% ratio, density of 2.5g/cm 3 The grain diameter is 100 μm, the pH value is 4.5, and a small part of impurities are inorganic substances P, F, cd, cu, zn, pb and organic substances C 4 H 8 O 2 S、C 4 H 4 N 2 OS 2 The ratio is 3%.|[0019] Further, in the second step and the third step, the grinding medium is in a proportion of 0.8mm:0.5mm: zirconia balls with 0.3 mm=1:2:2, the ball-to-material ratio is 7:2-4, and the rotating speed is adjusted to be 200 r/min-800 r/min.|[0020] Further, the CO introduced in the second step 2 CO trapping for purification of industrial process exhaust gas 2 The purity is more than or equal to 45 percent.|[0021] Further, in the third step, the crystal form control agent is an inorganic AlCl 3 The slurry is added with the concentration controlled between 0.30mol/L and 0.40mol/L, and the temperature is controlled between 60 ℃ and 80 ℃ by a constant temperature controller.|[0022] And in the third step, the crystal form control agent is an organic matter, ethanol solution with the concentration of 90 percent is added into the slurry according to the volume ratio of the ethanol solution to the ammonia water of 1:1-2, and the temperature is controlled at 40-60 ℃ by a constant temperature controller.|[0023] Further, in the third step, the crystal form control agent is AlCl 3 One of ethanol.|[0024] (III) beneficial effects|[0025] Compared with the prior art, the invention provides a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, which has the following beneficial effects:|[0026] 1. according to the method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, byproduct phosphogypsum is fully crushed through small-particle-size zirconia balls in a wet grinding stage, so that the contact area of ammonia water and phosphogypsum particles is increased, ion dissolution is improved, and CO is introduced into the solution 2 And (3) carbon fixation is carried out, so that the carbon fixation efficiency of solid waste is improved.|[0027] 2. The method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial by-product gypsum has the advantages of low raw material cost, low energy consumption, short time consumption and simple preparation process, and is favorable for industrial production.|[0028] 3. The method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum solves the problems of low utilization rate of industrial solid waste phosphogypsum and solidification of greenhouse gas CO during preparation of aragonite calcium carbonate 2 And the like.|[0029] 4. According to the method for preparing the nano-micron calcium carbonate by wet carbon fixation of the industrial byproduct gypsum, the purity of the gypsum can be improved by using a wet grinding impurity removal method, so that the carbon fixation efficiency and the calcium carbonate generation efficiency are improved.|DRAWINGS DESCRIPTION|[0030] FIG. 1 is a flow chart of the method of the present invention.|INVENTION MODE|Detailed Description|[0031] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0032] The main chemical components of the industrial byproduct gypsum subjected to impurity removal are uniformly described as follows: the industrial by-product gypsum with impurities removed used in the examples is solid waste in wet phosphoric acid process, and the components thereof are mainly CaSO 4 ·2H 2 O, with a 97% ratio, density of 2.5g/cm 3 The grain diameter is 100 μm, the pH value is 4.5, and a small part of impurities are inorganic substances P, F, cd, cu, zn, pb and organic substances C 4 H 8 O 2 S、C 4 H 4 N 2 OS 2 Etc. with a 3% ratio. CO used in the examples 2 CO trapping for purification of industrial production tail gas 2 The purity of the ammonia gas is more than or equal to 45%, the ammonia gas used in the examples is industrial production ammonia gas, the purity of the ammonia gas is more than or equal to 85%, the ammonia gas is extremely soluble in water, and the ammonia gas is not described in the examples.|[0033] Embodiment one: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0034] step one: introducing ammonia gas into water according to the gas-liquid volume ratio of 700:1, and fully dissolving the ammonia gas at normal temperature to obtain ammonia water with the concentration of about 20%;|[0035] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:2, adding a grinding medium, adjusting the rotating speed to 200r/min, performing wet grinding at about 20 ℃, and simultaneously introducing CO of 0.4MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0036] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.30mol/L, the temperature is controlled to be 60 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is regulated to have the rotating speed of 200r/min, wet grinding is continuously carried out, or ethanol solution with the volume ratio of the crystal form control agent to the ammonia water of about 1:1 and the concentration of 90 percent is immediately added after the wet grinding is stopped, the temperature is controlled to be 40 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is adjusted to have the rotating speed of 200r/min, and wet grinding is continuously carried out;|[0037] step four: wet grinding for 60min, pulping, sieving with 100 mesh square sieve to remove zirconia wet grinding ball, filtering, and drying to obtain aragonite type calcium carbonate.|[0038] Embodiment two: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0039] step one: ammonia is introduced into water according to the volume ratio of gas to liquid of 800:1, and is fully dissolved at normal temperature to obtain ammonia water with the concentration of about 25%;|[0040] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:3, adding a grinding medium, adjusting the rotating speed to 500r/min, performing wet grinding at about 30 ℃, and simultaneously introducing CO at 0.5MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0041] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.35mol/L, the temperature is controlled to be 65 ℃ by a constant temperature controller, and CO is continuously introduced 2 Gas, regulating the rotating speed to 500r/min, continuously carrying out wet grinding, or immediately adding ethanol solution with the volume ratio of the crystal form control agent to ammonia water of about 1:1.5 and the concentration of 90 percent after suspending the wet grinding, controlling the temperature at 45 ℃ by using a constant temperature controller, and continuously introducing CO 2 The gas is adjusted to have the rotating speed of 500r/min, and wet grinding is continuously carried out;|[0042] step four: wet grinding for about 75min, pulping and refining, sieving the slurry with 100 mesh square hole sieve to remove zirconia wet grinding balls, filtering, and drying to obtain aragonite type calcium carbonate.|[0043] Embodiment III: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0044] step one: ammonia is introduced into water according to the volume ratio of gas to liquid of 800:1, and is fully dissolved at normal temperature to obtain ammonia water with the concentration of about 25%;|[0045] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:3, adding a grinding medium, adjusting the rotating speed to 500r/min, performing wet grinding at about 30 ℃, and simultaneously introducing CO at 0.6MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0046] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.35mol/L, the temperature is controlled to be 70 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is regulated to rotate at 500r/min, wet grinding is continuously carried out, or ethanol solution with the volume ratio of crystal form control agent to ammonia water of about 1:1.5 and the concentration of 90% is added immediately after the wet grinding is stopped, the temperature is controlled at 50 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is adjusted to have the rotating speed of 500r/min, and wet grinding is continuously carried out;|[0047] step four: wet grinding for about 75min, pulping and refining, sieving the slurry with 100 mesh square hole sieve to remove zirconia wet grinding balls, filtering, and drying to obtain aragonite type calcium carbonate.|[0048] Embodiment four: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0049] step one: ammonia is introduced into water according to the volume ratio of gas to liquid of 800:1, and is fully dissolved at normal temperature to obtain ammonia water with the concentration of about 25%;|[0050] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:3, adding a grinding medium, adjusting the rotating speed to 500r/min, performing wet grinding at about 30 ℃, and simultaneously introducing CO at 0.7MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0051] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.35mol/L, the temperature is controlled to be 75 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is regulated to rotate at 500r/min, wet grinding is continuously carried out, or ethanol solution with the volume ratio of crystal form control agent to ammonia water of about 1:1.5 and the concentration of 90% is added immediately after the wet grinding is stopped, the temperature is controlled at 55 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is adjusted to have the rotating speed of 500r/min, and wet grinding is continuously carried out;|[0052] step four: wet grinding for about 75min, pulping and refining, sieving the slurry with 100 mesh square hole sieve to remove zirconia wet grinding balls, filtering, and drying to obtain aragonite type calcium carbonate.|[0053] Fifth embodiment: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0054] step one: introducing ammonia gas into water according to the volume ratio of gas to liquid of 900:1, and fully dissolving the ammonia gas at normal temperature to obtain ammonia water with the concentration of about 30%;|[0055] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:4, adding a grinding medium, adjusting the rotating speed to 800r/min, performing wet grinding at about 40 ℃, and simultaneously introducing CO at 0.8MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0056] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.40mol/L, the temperature is controlled to be 80 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is adjusted to have the rotating speed of 800r/min, and wet grinding is continuously carried out; or adding crystal form control agent and ammonia water immediately after suspending wet millingEthanol solution with volume ratio of about 1:2 and concentration of 90 percent is used for controlling the temperature at 60 ℃ by a constant temperature controller and continuously introducing CO 2 The gas is adjusted to have the rotating speed of 800r/min, and wet grinding is continuously carried out;|[0057] step four: wet grinding for about 80min, pulping and refining, sieving the slurry with 100 mesh square hole sieve to remove zirconia wet grinding balls, filtering, and drying to obtain aragonite type calcium carbonate.|[0058] Test data of the products obtained in examples one to five|[0059] |[0060] From the table in combination with the example data, it can be seen that example five resulted in aragonite CaCO due to increases in rotational speed, crystal form regulator concentration, carbon dioxide concentration, and temperature 3 The content is relatively maximum, the whiteness is relatively maximum, and CaCO is mixed 3 Particle size is relatively minimum, data is optimal, and example four comparative example five aragonite CaCO 3 Relatively low in content, relatively low in whiteness, and mixed with CaCO 3 The particle size is relatively large, but the practical utilization value of the fourth embodiment is high in the aspects of comprehensive energy consumption, raw material economy and the like, and the method is more suitable for industrial production, and the fourth embodiment is compared with the first embodiment, the second embodiment and the third embodiment, so that the method is not only used for aragonite CaCO 3 Higher content, smaller whiteness, aragonite CaCO 3 The particle size is smaller, the solid waste carbon fixation efficiency is higher, and the utilization rate of industrial solid waste phosphogypsum and greenhouse gas carbon dioxide is higher, so that the data scheme of the fourth embodiment is most suitable for actual production in comprehensive view, and the daily design requirement is met.|[0061] The reaction mechanism of the invention is as follows:|[0062] the invention provides a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, which comprises the steps of fully crushing shells of larger-particle calcium carbonate through zirconia balls with small particle size during carbon fixation to enable the shells to be continuously exposed out of fresh surfaces, generating calcium carbonate particles with smaller particle size, and simultaneously adding a crystal form regulator AlCl 3 One of the aluminum ions and the ethanol is adhered to the surface of the calcium carbonate to weaken the relative growth speed and reduceThe method has the advantages that the possibility of forming calcite calcium carbonate seed crystals or the solvation of ethanol is adopted to make the system in a low saturation state, create a microenvironment suitable for the formation of aragonite calcium carbonate, and in the continuous impact process, calcium carbonate with smaller particle size is formed to be more favorable for the adsorption of aluminum ions or improve the solvation of ethanol, so that the formation efficiency of aragonite calcium carbonate crystal forms is improved.|[0063] The beneficial effects of the invention are as follows:|[0064] according to the method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, byproduct phosphogypsum is fully crushed through small-particle-size zirconia balls in a wet grinding stage, so that the contact area of ammonia water and phosphogypsum particles is increased, ion dissolution is improved, and CO is introduced into the solution 2 And (3) carbon fixation is carried out, so that the carbon fixation efficiency of solid waste is improved.|[0065] And moreover, the raw materials are industrial byproduct gypsum, so that the raw material cost is low, the manufacturing energy consumption is low, the time consumption is short, the manufacturing process is simple, and the industrial production is facilitated.|[0066] Meanwhile, the method solves the problems of low utilization rate of industrial solid waste phosphogypsum and solidification of greenhouse gas CO while preparing aragonite type calcium carbonate 2 And the like.|[0067] In addition, the purity of gypsum can be improved by using a wet grinding impurity removal method, so that the carbon fixation efficiency and the calcium carbonate generation efficiency are improved.|[0068] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. (CN116177584)|TECHNICAL FIELD|[0001] The invention relates to the technical fields of resource utilization and environmental protection treatment of industrial by-product gypsum, in particular to a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial by-product gypsum.|BACKGROUND ART|[0002] Phosphogypsum refers to solid waste in the wet phosphoric acid process, and the chemical reaction equation is as follows: ca (Ca) 5 (PO 4 ) 3 X+5H 2 SO 4 +10H 2 O→3H 3 PO 4 +5(CaSO 4 ·2H 2 O) +HX, (wherein X can comprise OH, F, cl or Br), and according to investigation calculation, phosphogypsum is produced by 4 t-6 t per 1t of phosphoric acid production.|[0003] Calcium carbonate belongs to polytype crystal, mainly calcite, aragonite and vaterite are usually present in the most stable calcite form, so that the annual demand of calcium carbonate in China is very large at present, the application fields of calcium carbonate with different morphologies are continuously expanded, the most common morphology of calcium carbonate is spherical, needle-shaped, flaky, chain-locked, cubic, amorphous and the like, aragonite calcium carbonate is taken as an important inorganic product, is a high-performance novel composite material reinforcing and toughening agent, has a complete structure and fewer defects in the interior, can be used in the industries of daily plastics, rubber, papermaking and the like,|[0004] compared with common SiC and potassium titanate whiskers in the market, the aragonite calcium carbonate has the advantages of high whiteness, large filling amount and the like, and is relatively low in cost, and the special appearance and the high compatibility with matrix resin during compounding with plastics obviously improve the processing performance and mechanical properties of products, so that the aragonite calcium carbonate is widely applied to the fields of paint coatings, plastics, rubber, printing ink, papermaking, brake pads, frosted materials, daily chemicals, foods, medicines and the like.|[0005] The Chinese patent CN104790024A has been searched and a method for preparing aragonite type calcium carbonate whisker with high length-diameter ratio is disclosed, which comprises the steps of preparing Ca (OH) with 1.0-8.2wt% 2 Adding magnesium chloride as crystal form regulator into the suspension, introducing CO 2 And N 2 Carbonizing the mixed gas, and finally carrying out suction filtration, washing, drying and crushing to obtain aragonite type calcium carbonate with the length-diameter ratio of 10-26, wherein Ca (OH) is contained in the lime milk suspension by the method 2 The solid content is low, the production efficiency is low, the magnesium chloride consumption is relatively high, the cost is high, and the recovery is difficult.|[0006] Also, it is found that CN1641077 discloses a method for preparing aragonite type calcium carbonate whisker, which comprises preparing slurry from quicklime or slaked lime, using magnesium salt as crystal form control agent, and introducing CO 2 The aragonite calcium carbonate with 93-98% of content is obtained by carbonization, and the magnesium salt solution can be recycled, but the method needs to carry out sedimentation classification on slurry for 3 times, chemical analysis on magnesium salt recovery liquid and the like, has complex operation flow, long reaction time of 4 hours and multiple stages, has the combination rotating speed of 600r/min, and has overlarge energy consumption.|[0007] The literature for preparing the aragonite type calcium carbonate by wet-milling carbon fixation by utilizing the solid waste phosphogypsum is not searched, so the method aims to provide a method for preparing nano-micron calcium carbonate by wet-milling carbon fixation by utilizing industrial byproduct gypsum, and solves the problems of low utilization rate, environmental pollution and the like of the industrial solid waste phosphogypsum while preparing the aragonite type calcium carbonate, changes waste into valuable and solidifies greenhouse gas CO 2 The greenhouse effect is relieved.|DISCLOSURE|Disclosure of Invention|[0008] (one) solving the technical problems|[0009] Aiming at the defects of the prior art, the invention provides a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, which solves the problem of Ca (OH) in lime milk suspension 2 Low solid content, low production efficiency, relatively high magnesium chloride consumption, high cost and difficult recovery.|[0010] (II) technical scheme|[0011] In order to achieve the above purpose, the present invention provides the following technical solutions: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0012] step one: ammonia gas is introduced into water according to the gas-liquid volume ratio of 700-900:1, and ammonia water with the concentration of 20% -30% can be fully dissolved at normal temperature;|[0013] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill according to a solid-liquid mass ratio of 1:2-4, adding a grinding medium, carrying out wet grinding at 20-40 ℃, and simultaneously introducing CO of 0.4-0.8 MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0014] step three: immediately adding a crystal form regulator after suspending wet grinding, controlling the temperature by a constant temperature controller, and introducing CO 2 The gas is continuously subjected to wet grinding through a grinding medium;|[0015] step four: wet grinding for 60-90 min, pulping and refining, wet grinding to obtain grain size of 60-1000 nm, sieving the slurry with 100 mesh square sieve to eliminate wet zirconia grinding ball, filtering and drying to obtain aragonite calcium carbonate with purity of 85-95%.|[0016] Further, the ammonia gas in the first step is industrial production ammonia gas, the purity is more than or equal to 85 percent, the ammonia gas is very easy to be dissolved in water, and the pH value of the ammonia water with the concentration of 20 to 30 percent is 9 to 10.|[0017] And further, the impurity removing method in the second step is to take a proper amount of byproduct gypsum, add a chemical cosolvent, a physical adsorbent, a chemical curing agent and a crystal form regulator to perform wet grinding, and perform solid-liquid separation and drying after the reaction is completed, thus obtaining the gypsum.|[0018] Further, the step two is describedThe industrial byproduct gypsum is mainly phosphogypsum, is solid waste in the wet phosphoric acid process, and mainly comprises CaSO as the component 4 ·2H 2 O, with a 97% ratio, density of 2.5g/cm 3 The grain diameter is 100 μm, the pH value is 4.5, and a small part of impurities are inorganic substances P, F, cd, cu, zn, pb and organic substances C 4 H 8 O 2 S、C 4 H 4 N 2 OS 2 The ratio is 3%.|[0019] Further, in the second step and the third step, the grinding medium is in a proportion of 0.8mm:0.5mm: zirconia balls with 0.3 mm=1:2:2, the ball-to-material ratio is 7:2-4, and the rotating speed is adjusted to be 200 r/min-800 r/min.|[0020] Further, the CO introduced in the second step 2 CO trapping for purification of industrial process exhaust gas 2 The purity is more than or equal to 45 percent.|[0021] Further, in the third step, the crystal form control agent is an inorganic AlCl 3 The slurry is added with the concentration controlled between 0.30mol/L and 0.40mol/L, and the temperature is controlled between 60 ℃ and 80 ℃ by a constant temperature controller.|[0022] And in the third step, the crystal form control agent is an organic matter, ethanol solution with the concentration of 90 percent is added into the slurry according to the volume ratio of the ethanol solution to the ammonia water of 1:1-2, and the temperature is controlled at 40-60 ℃ by a constant temperature controller.|[0023] Further, in the third step, the crystal form control agent is AlCl 3 One of ethanol.|[0024] (III) beneficial effects|[0025] Compared with the prior art, the invention provides a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, which has the following beneficial effects:|[0026] 1. according to the method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, byproduct phosphogypsum is fully crushed through small-particle-size zirconia balls in a wet grinding stage, so that the contact area of ammonia water and phosphogypsum particles is increased, ion dissolution is improved, and CO is introduced into the solution 2 And (3) carbon fixation is carried out, so that the carbon fixation efficiency of solid waste is improved.|[0027] 2. The method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial by-product gypsum has the advantages of low raw material cost, low energy consumption, short time consumption and simple preparation process, and is favorable for industrial production.|[0028] 3. The method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum solves the problems of low utilization rate of industrial solid waste phosphogypsum and solidification of greenhouse gas CO during preparation of aragonite calcium carbonate 2 And the like.|[0029] 4. According to the method for preparing the nano-micron calcium carbonate by wet carbon fixation of the industrial byproduct gypsum, the purity of the gypsum can be improved by using a wet grinding impurity removal method, so that the carbon fixation efficiency and the calcium carbonate generation efficiency are improved.|DRAWINGS DESCRIPTION|[0030] FIG. 1 is a flow chart of the method of the present invention.|INVENTION MODE|Detailed Description|[0031] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0032] The main chemical components of the industrial byproduct gypsum subjected to impurity removal are uniformly described as follows: the industrial by-product gypsum with impurities removed used in the examples is solid waste in wet phosphoric acid process, and the components thereof are mainly CaSO 4 ·2H 2 O, with a 97% ratio, density of 2.5g/cm 3 The grain diameter is 100 μm, the pH value is 4.5, and a small part of impurities are inorganic substances P, F, cd, cu, zn, pb and organic substances C 4 H 8 O 2 S、C 4 H 4 N 2 OS 2 Etc. with a 3% ratio. CO used in the examples 2 CO trapping for purification of industrial production tail gas 2 The purity of the ammonia gas is more than or equal to 45%, the ammonia gas used in the examples is industrial production ammonia gas, the purity of the ammonia gas is more than or equal to 85%, the ammonia gas is extremely soluble in water, and the ammonia gas is not described in the examples.|[0033] Embodiment one: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0034] step one: introducing ammonia gas into water according to the gas-liquid volume ratio of 700:1, and fully dissolving the ammonia gas at normal temperature to obtain ammonia water with the concentration of about 20%;|[0035] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:2, adding a grinding medium, adjusting the rotating speed to 200r/min, performing wet grinding at about 20 ℃, and simultaneously introducing CO of 0.4MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0036] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.30mol/L, the temperature is controlled to be 60 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is regulated to have the rotating speed of 200r/min, wet grinding is continuously carried out, or ethanol solution with the volume ratio of the crystal form control agent to the ammonia water of about 1:1 and the concentration of 90 percent is immediately added after the wet grinding is stopped, the temperature is controlled to be 40 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is adjusted to have the rotating speed of 200r/min, and wet grinding is continuously carried out;|[0037] step four: wet grinding for 60min, pulping, sieving with 100 mesh square sieve to remove zirconia wet grinding ball, filtering, and drying to obtain aragonite type calcium carbonate.|[0038] Embodiment two: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0039] step one: ammonia is introduced into water according to the volume ratio of gas to liquid of 800:1, and is fully dissolved at normal temperature to obtain ammonia water with the concentration of about 25%;|[0040] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:3, adding a grinding medium, adjusting the rotating speed to 500r/min, performing wet grinding at about 30 ℃, and simultaneously introducing CO at 0.5MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0041] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.35mol/L, the temperature is controlled to be 65 ℃ by a constant temperature controller, and CO is continuously introduced 2 Gas, regulating the rotating speed to 500r/min, continuously carrying out wet grinding, or immediately adding ethanol solution with the volume ratio of the crystal form control agent to ammonia water of about 1:1.5 and the concentration of 90 percent after suspending the wet grinding, controlling the temperature at 45 ℃ by using a constant temperature controller, and continuously introducing CO 2 The gas is adjusted to have the rotating speed of 500r/min, and wet grinding is continuously carried out;|[0042] step four: wet grinding for about 75min, pulping and refining, sieving the slurry with 100 mesh square hole sieve to remove zirconia wet grinding balls, filtering, and drying to obtain aragonite type calcium carbonate.|[0043] Embodiment III: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0044] step one: ammonia is introduced into water according to the volume ratio of gas to liquid of 800:1, and is fully dissolved at normal temperature to obtain ammonia water with the concentration of about 25%;|[0045] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:3, adding a grinding medium, adjusting the rotating speed to 500r/min, performing wet grinding at about 30 ℃, and simultaneously introducing CO at 0.6MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0046] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.35mol/L, the temperature is controlled to be 70 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is regulated to rotate at 500r/min, wet grinding is continuously carried out, or ethanol solution with the volume ratio of crystal form control agent to ammonia water of about 1:1.5 and the concentration of 90% is added immediately after the wet grinding is stopped, the temperature is controlled at 50 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is adjusted to have the rotating speed of 500r/min, and wet grinding is continuously carried out;|[0047] step four: wet grinding for about 75min, pulping and refining, sieving the slurry with 100 mesh square hole sieve to remove zirconia wet grinding balls, filtering, and drying to obtain aragonite type calcium carbonate.|[0048] Embodiment four: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0049] step one: ammonia is introduced into water according to the volume ratio of gas to liquid of 800:1, and is fully dissolved at normal temperature to obtain ammonia water with the concentration of about 25%;|[0050] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:3, adding a grinding medium, adjusting the rotating speed to 500r/min, performing wet grinding at about 30 ℃, and simultaneously introducing CO at 0.7MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0051] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.35mol/L, the temperature is controlled to be 75 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is regulated to rotate at 500r/min, wet grinding is continuously carried out, or ethanol solution with the volume ratio of crystal form control agent to ammonia water of about 1:1.5 and the concentration of 90% is added immediately after the wet grinding is stopped, the temperature is controlled at 55 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is adjusted to have the rotating speed of 500r/min, and wet grinding is continuously carried out;|[0052] step four: wet grinding for about 75min, pulping and refining, sieving the slurry with 100 mesh square hole sieve to remove zirconia wet grinding balls, filtering, and drying to obtain aragonite type calcium carbonate.|[0053] Fifth embodiment: a method for preparing nano-micron calcium carbonate by industrial byproduct gypsum wet carbon fixation comprises the following steps:|[0054] step one: introducing ammonia gas into water according to the volume ratio of gas to liquid of 900:1, and fully dissolving the ammonia gas at normal temperature to obtain ammonia water with the concentration of about 30%;|[0055] step two: adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill at a solid-liquid mass ratio of 1:4, adding a grinding medium, adjusting the rotating speed to 800r/min, performing wet grinding at about 40 ℃, and simultaneously introducing CO at 0.8MPa 2 Carrying out carbon fixation reaction on the gas, grinding until the pH value is 9, and suspending wet grinding;|[0056] step three: adding crystal form regulator to stop wet milling to obtain AlCl 3 The concentration is controlled to be 0.40mol/L, the temperature is controlled to be 80 ℃ by a constant temperature controller, and CO is continuously introduced 2 The gas is adjusted to have the rotating speed of 800r/min, and wet grinding is continuously carried out; or adding crystal form control agent and ammonia water immediately after suspending wet millingEthanol solution with volume ratio of about 1:2 and concentration of 90 percent is used for controlling the temperature at 60 ℃ by a constant temperature controller and continuously introducing CO 2 The gas is adjusted to have the rotating speed of 800r/min, and wet grinding is continuously carried out;|[0057] step four: wet grinding for about 80min, pulping and refining, sieving the slurry with 100 mesh square hole sieve to remove zirconia wet grinding balls, filtering, and drying to obtain aragonite type calcium carbonate.|[0058] Test data of the products obtained in examples one to five|[0059] |[0060] From the table in combination with the example data, it can be seen that example five resulted in aragonite CaCO due to increases in rotational speed, crystal form regulator concentration, carbon dioxide concentration, and temperature 3 The content is relatively maximum, the whiteness is relatively maximum, and CaCO is mixed 3 Particle size is relatively minimum, data is optimal, and example four comparative example five aragonite CaCO 3 Relatively low in content, relatively low in whiteness, and mixed with CaCO 3 The particle size is relatively large, but the practical utilization value of the fourth embodiment is high in the aspects of comprehensive energy consumption, raw material economy and the like, and the method is more suitable for industrial production, and the fourth embodiment is compared with the first embodiment, the second embodiment and the third embodiment, so that the method is not only used for aragonite CaCO 3 Higher content, smaller whiteness, aragonite CaCO 3 The particle size is smaller, the solid waste carbon fixation efficiency is higher, and the utilization rate of industrial solid waste phosphogypsum and greenhouse gas carbon dioxide is higher, so that the data scheme of the fourth embodiment is most suitable for actual production in comprehensive view, and the daily design requirement is met.|[0061] The reaction mechanism of the invention is as follows:|[0062] the invention provides a method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, which comprises the steps of fully crushing shells of larger-particle calcium carbonate through zirconia balls with small particle size during carbon fixation to enable the shells to be continuously exposed out of fresh surfaces, generating calcium carbonate particles with smaller particle size, and simultaneously adding a crystal form regulator AlCl 3 One of the aluminum ions and the ethanol is adhered to the surface of the calcium carbonate to weaken the relative growth speed and reduceThe method has the advantages that the possibility of forming calcite calcium carbonate seed crystals or the solvation of ethanol is adopted to make the system in a low saturation state, create a microenvironment suitable for the formation of aragonite calcium carbonate, and in the continuous impact process, calcium carbonate with smaller particle size is formed to be more favorable for the adsorption of aluminum ions or improve the solvation of ethanol, so that the formation efficiency of aragonite calcium carbonate crystal forms is improved.|[0063] The beneficial effects of the invention are as follows:|[0064] according to the method for preparing nano-micron calcium carbonate by wet carbon fixation of industrial byproduct gypsum, byproduct phosphogypsum is fully crushed through small-particle-size zirconia balls in a wet grinding stage, so that the contact area of ammonia water and phosphogypsum particles is increased, ion dissolution is improved, and CO is introduced into the solution 2 And (3) carbon fixation is carried out, so that the carbon fixation efficiency of solid waste is improved.|[0065] And moreover, the raw materials are industrial byproduct gypsum, so that the raw material cost is low, the manufacturing energy consumption is low, the time consumption is short, the manufacturing process is simple, and the industrial production is facilitated.|[0066] Meanwhile, the method solves the problems of low utilization rate of industrial solid waste phosphogypsum and solidification of greenhouse gas CO while preparing aragonite type calcium carbonate 2 And the like.|[0067] In addition, the purity of gypsum can be improved by using a wet grinding impurity removal method, so that the carbon fixation efficiency and the calcium carbonate generation efficiency are improved.|[0068] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. Family Number|(105110541)|105110541|Abstract|(CN116177584 A)|The invention relates to the technical field of resource utilization of industrial by - product gypsum and environmental protection and treatment , and discloses a method for preparing nano - micron calcium carbonate by wet carbon sequestration of industrial by - product gypsum , which comprises the following steps : 1, introducing ammonia gas into water according to a gas - liquid volume ratio of ( 700-900 ) : 1, the mixture can be fully dissolved at normal temperature to obtain ammonia water with the concentration of 20%-30% ; 2, adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill according to the solid - liquid mass ratio of 1 : ( 2-4 ) , adding a grinding medium , carrying out wet grinding at the temperature of about 20-40 DEG C , introducing 0.4-0.8 MPa CO2 gas to carry out a carbon sequestration reaction , grinding until the pH value is 9, and suspending wet grinding ; according to the method for preparing the nano - micron calcium carbonate through wet carbon sequestration of the industrial byproduct gypsum , the byproduct phosphogypsum is fully crushed through the small - particle - size zirconium oxide balls in the wet grinding stage , the contact area of ammonia water and phosphogypsum particles is increased , ion dissolution is improved , CO2 is introduced into a solution for carbon sequestration , and the solid waste carbon sequestration efficiency is improved . |CPC codes|(CN116177584 A)|C01F - 011/18/2 |C01F - 011/18/3 |C01F - 011/46/8 |C01P - 2004/62 |C01P - 2004/64 |C01P - 2006/60 |C01P - 2006/80 |IPC codes|(CN116177584 A)|C01F - 011/18 |C01F - 011/46 |Title|(CN116177584 A)|Method for preparing nano - micron calcium carbonate by wet carbon sequestration of industrial byproduct gypsum | Chemical engineering|Materials, metallurgy|Micro-structure and nano-technology B02C-017/10|B02C-017/20|B82Y-030/00|B82Y-040/00|C01F-011/18/2|C01F-011/18/3|C01F-011/46/8|C01P-2004/62|C01P-2004/64|C01P-2006/60|C01P-2006/80|Y02P-020/141 B02C-017/10|B02C-017/20|B82Y-030/00|B82Y-040/00|C01F-011/18/2|C01F-011/18/3|C01F-011/46/8|C01P-2004/62|C01P-2004/64|C01P-2006/60|C01P-2006/80|Y02P-020/141 B02C-017/10|B02C-017/20|B82Y-030/00|B82Y-040/00|C01F-011/18|C01F-011/46 B02C-017/10|B02C-017/20|B82Y-030/00|B82Y-040/00|C01F-011/18|C01F-011/46 CN117983637|CN117185755 CN117983637 109684237 WHO=Examiner SELF=N CAT=A|CN117185755 107666134 WHO=Examiner SELF=N CAT=A CN114906868|CN115215586|KR101666208|CN114956759|CN108192696 CN114906868 101342271 WHO=Examiner SELF=Y CAT=Y|CN115215586 102252310 WHO=Examiner SELF=Y CAT=Y|KR101666208 74446904 WHO=Examiner SELF=N CAT=Y|CN114956759 101540849 WHO=Examiner SELF=Y CAT=A|CN108192696 80159737 WHO=Examiner SELF=N CAT=A 冯臻: &quot;文石晶须的研究&quot;, 化工矿物与加工, no. 08, 25 August 2002 (2002-08-25) (Cat. Y)|杨红;金达莱;马照军;姚奎鸿;: &quot;醇类添加剂对碳酸钙形貌及晶型的影响&quot;, 浙江理工大学学报, no. 05, 10 September 2007 (2007-09-10) (Cat. A) KR101666208; CN108192696; CN114906868; CN114956759; CN115215586 REVOKED (CN116177584)|REVOKED DEAD (CN116177584)|DEAD (CN116177584)|LEGAL DETAILS FOR CN116177584|Actual or expected expiration date=2025-06-24|Legal state=DEAD|Status=REVOKED|Event publication date=2023-03-06|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202310205812|Application date=2023-03-06|Standardized application number=2023CN-0205812|Event publication date=2023-05-30|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN116177584|Publication stage code=A|Publication date=2023-05-30|Standardized publication number=CN116177584|Event publication date=2023-05-30|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-06-16|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-06-24|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQx9ffYl3p7MVfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067999919&ekey=1900&xpn=CN116177584&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=sE1KaaYuF081YOhgzqmUGJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN116177584)|CN (CN116177584)|NAME=HUBEI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN116177584)|NAME=HUANG DINGJIN;WUHAN SINOPOWER PATENT AGENCY , REG=42237 (CN116177584)|NAME=SU YING|NAME=GUANG LUN|NAME=HE XINGYANG|NAME=YANG JIN|NAME=DAI FEI|NAME=ZHENG ZHENGQI|NAME=BAI SHIYING|NAME=WAN ZIHENG 0 1 Titre: (CN116177584)|Method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial byproduct gypsum Résumé: (CN116177584)|The invention relates to the technical field of resource utilization of industrial by-product gypsum and environmental protection and treatment, and discloses a method for preparing nano-micron calcium carbonate by wet carbon sequestration of industrial by-product gypsum, which comprises the following steps: 1, introducing ammonia gas into water according to a gas-liquid volume ratio of (700-900): 1, the mixture can be fully dissolved at normal temperature to obtain ammonia water with the concentration of 20%-30%; 2, adding the industrial byproduct gypsum subjected to impurity removal and prepared ammonia water into a wet mill according to the solid-liquid mass ratio of 1: (2-4), adding a grinding medium, carrying out wet grinding at the temperature of about 20-40 DEG C, introducing 0.4-0.8 MPa CO2 gas to carry out a carbon sequestration reaction, grinding until the pH value is 9, and suspending wet grinding; according to the method for preparing the nano-micron calcium carbonate through wet carbon sequestration of the industrial byproduct gypsum, the byproduct phosphogypsum is fully crushed through the small-particle-size zirconium oxide balls in the wet grinding stage, the contact area of ammonia water and phosphogypsum particles is increased, ion dissolution is improved, CO2 is introduced into a solution for carbon sequestration, and the solid waste carbon sequestration efficiency is improved. 26 Abstract gpt-4o-mini no The focus is on carbon sequestration using industrial by-product gypsum to produce calcium carbonate, not on accelerating the weathering of silicate or alkaline minerals for CO₂ capture.
29 CN202510587920 CN202510587920 CN120349127 115363993 CN120349127 A 2025-07-22 [CN120349127] 2025-05-08 2025-05-08 2025-07-22 (CN120349127)|2045-05-08 (CN120349127)|Carbon sequestration strengthening method and carbonization calculation method of cement-based material (CN120349127)|The invention discloses a carbon sequestration strengthening method of a cement-based material and a carbonization calculation method of the cement-based material, and belongs to the technical field of cement-based material preparation. The preparation method comprises the following steps: fully soaking dried straws in a mixed alkaline aqueous solution containing titanium dioxide and ruthenium chloride, putting the straws in a freeze dryer for quick-freezing, drying and crushing, and fully carbonizing in a nitrogen atmosphere to form bimetallic modified straw derived carbon material powder; adding the straw derived carbon material powder into a cement-based material, and uniformly mixing to form slurry; and pouring the slurry into a standard mold for curing. The titanium and ruthenium modified straw derivative material is introduced into the cement-based material, the contact area of the cement-based material and carbon dioxide is kept, carbon sequestration is conducted on the cement-based material through photocatalysis in the natural use process, the durability and carbonization performance of the cement-based material can be improved, and meanwhile the provided carbonization calculation method is easy to operate and low in cost. And the precision of evaluating the carbonization of the cement-based material is effectively improved. SHENZHEN UNIVERSITY (CN120349127)|SHENZHEN UNIVERSITY ([CN]) LIU JUN|ZHENG WENTAO|ZHANG WEIZHUO|CHENG LEI|OU GUANGMING (CN120349127)|LIU JUN|ZHENG WENTAO|ZHANG WEIZHUO|CHENG LEI|OU GUANGMING (CN120349127)|ZHAO RONG;BEIJING ZHIYI INTERNET INTELLECTUAL PROPERTY AGENCY CO., LTD|Reg. Nb: 16137 (CN120349127)|1. The carbon fixation strengthening method of the cement-based material is characterized by comprising the following steps of: S1, fully soaking the dried straw in a mixed alkaline aqueous solution containing titanium dioxide and ruthenium chloride, then placing the straw in a freeze dryer for quick freeze drying and crushing, and fully carbonizing the straw in a nitrogen atmosphere to form bimetal modified straw derived carbon material powder; s2, adding straw derived carbon material powder into a cement-based material, uniformly mixing to form slurry, controlling the water-glue ratio to be fixed at 0.4-0.6, and controlling the glue-sand ratio to be 1 (2-4); S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃.| (CN120349127)|The invention aims to provide a carbon fixation strengthening method of a cement-based material and a carbonization calculation method thereof, wherein a titanium and ruthenium modified straw derivative material is introduced into the cement-based material, so that the contact area of the cement-based material and carbon dioxide is maintained, the cement-based material is subjected to carbon fixation by photocatalysis in natural use, the durability and carbonization performance of the cement-based material are improved, and meanwhile, the provided carbonization calculation method is simple to operate, and the accuracy of evaluating the carbonization of the cement-based material is effectively improved.In order to achieve the above object, the present invention provides a carbon sequestration strengthening method for cement-based materials, comprising the steps of:|The invention discloses a carbon fixation strengthening method of a cement-based material and a carbonization calculating method thereof, belonging to the technical field of cement-based material preparation.|The invention relates to the technical field of cement-based material preparation, in particular to a carbon fixation strengthening method of a cement-based material and a carbonization calculation method thereof.| (CN120349127)|CEMENT MATERIAL(100,63)|CARBON FIXATION(100,17)|CARBONIZATION CALCULATION(100,12)|ALKALINE AQUEOUS SOLUTION(37,11)|DRIED STRAW(36,6)|CARBONIZATION PERFORMANCE(36,4)|CARBONATION CALCULATION(35,1)|PHOTOCATALYSIS(31,3)|CARBON SEQUESTRATION(30,6)|NITROGEN ATMOSPHERE(30,6)|MIXED ALKALINE AQUEOUS SOLUTION(29,11)|CRUSHING(29,5)|QUICK FREEZE DRYING(28,2)|REINFORCING CARBON FIXATION(28,2)|CEMENTITIOUS MATERIAL STRENGTHENING(27,2)|POWERFUL BLOWER(27,2)|SLURRY(26,13)|FREEZE DRYER(26,8)|STRAW(26,8)|DURABILITY(26,3)|STRAW DERIVED CARBON(25,6)|RUTHENIUM(25,3)|SAMPLE CARBONIZATION(24,2)|STANDARD MOLDING(23,7)|ARTIFICIAL AGGREGATE PARTICLE DIAMETER(23,2)|CEMENTITIOUS MATERIAL CALCULATING CARBONATION(23,1)|CEMENT MATERIAL CARBONIZATION PERFORMANCE(22,3)|RUTHENIUM CHLORIDE(21,8)|CEMENT MATERIAL CARBONIZATION(21,2)|GLUE SAND RATIO(21,2)|NONCOLORED REGION WIDTH(21,1)|CURING(20,9)|MODIFIED STRAW DERIVATIVE MATERIAL(19,2)|TITANIUM DIOXIDE(18,10)|CEMENT MATERIAL CARBONIZATION PRECISION(18,2)|STRAW DERIVATIVE MATERIAL(17,6)|PHENOLPHTHALEIN SOLUTION(17,3)|MEDIAN RATIO(17,2)|HEAT PRESERVATION(15,5)|MIXED AQUEOUS SOLUTION(15,4)|CARBONIZATION DEGREE CALCULATION(15,2)|CARBONIZATION TEMPERATURE(15,2)|NONCOLORED REGION AREA(14,1)|RUTHENIUM CHLORIDE MOLAR CONCENTRATION(13,2)|STRAW WEIGHT RATIO(13,2)|STRAW DERIVATIVE CARBON MATERIAL(13,1)|COLOR DEVELOPMENT AREA(12,4)|CARBON DIOXIDE(11,5)|WATER GLUE RATIO(11,2)|STRAW DERIVED CARBON MATERIAL(10,10)|MATERIAL POWDER(10,7)|SAMPLE CLEANING SECTION(10,2)|STRAW SOAKING TIME(10,2)|SOLID DRY ICE(9,8)|CEMENT MATERIAL CARBONIZATION CALCULATION(9,5)|DAILY(9,2)|MEDIUM SPEED FREEZE DRYING(9,1)|CONTACT AREA(8,4)|TEST SPECIMEN(8,4)|CURING(8,2)|PROVIDED CARBONIZATION CALCULATION(8,2)|GLOBAL ARTIFICIAL EMISSION(8,1)|EXPOSED SURFACE(7,4)|TITANIUM DIOXIDE VOLUME CONCENTRATION(7,2)|CARBONATE MINERAL DECOMPOSITION(7,1)|REALIZING CARBONIZATION(7,1)|MASS RATIO(6,7)|RELATIVE HUMIDITY(6,6)|STANDARD CURING(6,4)|PORE CANAL(6,1)|ACCOUNTING(5,3)|BIMETAL(5,3)|CEMENT MATERIAL CONTACT AREA(5,3)|ILLUMINATION(5,3)|MODIFIED STRAW DERIVED CARBON(5,3)|CARBON MATERIAL POWDER(5,2)|CARBONIZATION DEPTH(5,1)|CEMENT MATRIX(5,1)|PHOTOCATALYSIS CARBON FIXATION(5,1)|REINFORCING CARBON SEQUESTRATION(5,1)| (CN120349127)|1. The carbon fixation strengthening method of the cement-based material is characterized by comprising the following steps of:| S1, fully soaking the dried straw in a mixed alkaline aqueous solution containing titanium dioxide and ruthenium chloride, then placing the straw in a freeze dryer for quick freeze drying and crushing, and fully carbonizing the straw in a nitrogen atmosphere to form bimetal modified straw derived carbon material powder; | s2, adding straw derived carbon material powder into a cement-based material, uniformly mixing to form slurry, controlling the water-glue ratio to be fixed at 0.4-0.6, and controlling the glue-sand ratio to be 1 (2-4); | S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃. |2. The carbon sequestration strengthening method of cement-based materials according to claim 1, wherein in step S1, the molar concentration of ruthenium chloride in the mixed alkaline aqueous solution is 1-2 mmol/L, the volume concentration of titanium dioxide is 5-20 g/L, the weight ratio of straw in the mixed aqueous solution is 1 (2-2.5), and the pH of the mixed alkaline aqueous solution is 9-10.|3. The method for reinforcing carbon fixation of a cement-based material according to claim 1, wherein in the step S1, the soaking time of the straw in the mixed aqueous solution is 2-8 hours, the temperature of a freeze dryer is minus 60-20 ℃, the size after crushing is less than 10mm, the carbonization temperature is 500-800 ℃, the time is 2-6 hours, and the heat preservation is 2 hours.|4. The method for carbon sequestration strengthening of cementitious materials as defined in claim 1, wherein in step S2, the mass ratio of the straw-derived carbon material powder to the cementitious material is 1 (50-200).|5. The method for reinforcing carbon fixation of a cement-based material according to claim 1, wherein in the step S2, solid dry ice is uniformly added in the mixing process of the straw-derived carbon material powder and the cement-based material, and the mass ratio of the solid dry ice to the cement-based material is (0.2-3): 100.|6. The method for carbon sequestration strengthening of cementitious materials as defined in claim 1, wherein in step S3, at least 5 hours of light is applied daily during the curing process.|7. A cement-based material, characterized in that it is prepared by a carbon sequestration strengthening method of a cement-based material according to any one of claims 1 to 6.|8. A method of calculating carbonation of a cementitious material in accordance with claim 7 including the steps of:| (1) Crushing the cement-based material after curing for 28d into a sample with the particle size of 1cm-3cm, and using a press to break the sample along the middle and select the exposed surface for calculating the carbonization degree; | (2) Cleaning dust generated by breaking the sample on the exposed surface by using a powerful blower; | (3) Selecting phenolphthalein solution as an indicator to be sprayed on the cleaned sample section; | (4) Measuring the particle size of the sample and the width of the color development area along the center line of the section of the sample, and measuring the particle size of the artificial aggregate and the width of the color development area along the center lines in different directions again; | (5) The degree of carbonization of the samples was evaluated. |9. The method according to claim 8, wherein in the step (5), the average value of the particle diameters of the samples in different directions in the average ratio of the widths of the non-colored regions on the different center lines is calculated, or the square of the average value of the particle diameters of the artificial aggregate in the average ratio of the areas of the non-colored regions is calculated. (CN120349127)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of cement-based material preparation, in particular to a carbon fixation strengthening method of a cement-based material and a carbonization calculation method thereof.|BACKGROUND ART|[0002] With the increasing global warming problem, low-carbon, environment-friendly and sustainable development is a target for pursuit by various countries. The traditional building material industry, especially the cement industry, has high carbon emissions due to the combustion of fossil fuels and the decomposition of carbonate minerals to produce CO 2 during production. The carbon emission of the cement industry accounts for 6-7% of the global artificial emission and is a typical high carbon emission industry. The cement-based carbon fixation strengthening method mainly adopts a carbon fixation maintenance technology to absorb and solidify CO 2 in the using stage of cement, so that the carbon footprint of the cement in the whole life cycle is reduced. The method not only helps to reduce carbon emissions, but also improves the performance of the cement-based material.|[0003] Therefore, the exploration of the carbon fixation strengthening method and the carbonization calculation method of the cement-based material is of great significance for realizing low carbonization and green of the field of building materials.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a carbon fixation strengthening method of a cement-based material and a carbonization calculation method thereof, wherein a titanium and ruthenium modified straw derivative material is introduced into the cement-based material, so that the contact area of the cement-based material and carbon dioxide is maintained, the cement-based material is subjected to carbon fixation by photocatalysis in natural use, the durability and carbonization performance of the cement-based material are improved, and meanwhile, the provided carbonization calculation method is simple to operate, and the accuracy of evaluating the carbonization of the cement-based material is effectively improved.|[0005] In order to achieve the above object, the present invention provides a carbon sequestration strengthening method for cement-based materials, comprising the steps of:|[0006] S1, fully soaking the dried straw in a mixed alkaline aqueous solution containing titanium dioxide and ruthenium chloride, then placing the straw in a freeze dryer for quick freeze drying and crushing, and fully carbonizing the straw in a nitrogen atmosphere to form bimetal modified straw derived carbon material powder; |[0007] s2, adding straw derived carbon material powder into a cement-based material, uniformly mixing to form slurry, controlling the water-glue ratio to be fixed at 0.4-0.6, and controlling the glue-sand ratio to be 1 (2-4); |[0008] S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃. |[0009] Preferably, in the step S1, the molar concentration of ruthenium chloride in the mixed alkaline aqueous solution is 1-2 mmol/L, the volume concentration of titanium dioxide is 5-20 g/L, the weight ratio of straw in the mixed aqueous solution is 1 (2-2.5), and the pH of the mixed alkaline aqueous solution is 9-10.|[0010] Preferably, in the step S1, the soaking time of the straw in the mixed aqueous solution is 2-8 hours, the temperature of a freeze dryer is minus 60-minus 20 ℃, the size after crushing is smaller than 10mm, the carbonization temperature is 500-800 ℃, the time is 2-6 hours, and the heat preservation is carried out for 2 hours.|[0011] Preferably, in the step S2, the mass ratio of the straw-derived carbon material powder to the cement-based material is 1 (50-200).|[0012] Preferably, in the step S2, solid dry ice is uniformly added in the mixing process of the straw derived carbon material powder and the cement-based material, and the mass ratio of the solid dry ice to the cement-based material is (0.2-3): 100.|[0013] Preferably, in step S3, at least 5 hours of light is irradiated daily during the curing process.|[0014] The invention also provides a cement-based material prepared by the method.|[0015] The invention also provides a carbonization calculation method of the cement-based material, which comprises the following steps:|[0016] (1) Crushing the cement-based material after curing for 28d into a sample with the particle size of 1cm-3cm, and using a press to break the sample along the middle and select the exposed surface for calculating the carbonization degree; |[0017] (2) Cleaning dust generated by breaking the sample on the exposed surface by using a powerful blower; |[0018] (3) Selecting phenolphthalein solution as an indicator to be sprayed on the cleaned sample section; |[0019] (4) Measuring the particle size of the sample and the width of the color development area along the center line of the section of the sample, and measuring the particle size of the artificial aggregate and the width of the color development area along the center lines in different directions again; |[0020] (5) The degree of carbonization of the samples was evaluated. |[0021] Preferably, in the step (5), the evaluation method is that the average value of the particle diameters of the samples in different directions on the average value ratio of the widths of the non-color-developing areas on different central lines is calculated, or the square of the average value of the particle diameters of the artificial aggregates on the average value ratio of the areas of the non-color-developing areas is calculated.|[0022] Therefore, the carbon fixation strengthening method and the carbonization calculation method of the cement-based material have the following beneficial effects:|[0023] (1) According to the invention, the straw derivative material is introduced into the cement-based material, so that the advantage of the void structure of the straw is maintained, and the pore canal which is favorable for carbon dioxide transmission is formed in the cement matrix, so that the contact area, carbonization depth and area of the cement-based material and carbon dioxide can be effectively increased, and the carbonization performance and durability of the material are improved. |[0024] (2) According to the invention, titanium dioxide is introduced into the straw derivative material, and photocatalysis carbon fixation is used for a long time in the cement-based material, so that the method has the remarkable energy-saving advantage, is convenient to implement, widens the natural carbon fixation process, ensures the dispersion of the titanium dioxide, and improves the abundance of active sites of the straw derivative material.|[0025] (3) The invention provides a carbonization calculation method of cement-based materials, which is simple to operate, and can quantitatively measure the carbonization degree of the cement-based materials in different curing stages, thereby effectively improving the accuracy of evaluating the carbonization of the cement-based materials.|[0026] The technical scheme of the invention is further described in detail through the drawings and the embodiments.|DRAWINGS DESCRIPTION|[0027] FIG. 1is a schematic diagram showing the results of a method for calculating carbonization of a cement-based material after carbon sequestration reinforcement according to an embodiment of the present invention;|[0028] FIG. 2 shows carbonization results of the inventive examples one-three and the comparative examples at 7 days, 14 days, and 28 days of curing age; |[0029] reference numerals |[0030] A. Sample, carbonized area, C, non-carbonized area, 1-1, first axis, 2-2, second axis, 3-3, third axis, 4-4, fourth axis, di, sample particle size, di, dyeing particle size.|INVENTION MODE|Detailed Description|[0031] The technical scheme of the invention is further described below through the attached drawings and the embodiments.|[0032] The technical scheme of the invention is further described below through the attached drawings and the embodiments.|[0033] Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs.|[0034] Furthermore, it should be understood that although the present disclosure describes embodiments, not every embodiment is provided with a separate embodiment, and that this description is provided for clarity only, and that the disclosure is not limited to the embodiments described in detail below, and that the embodiments described in the examples may be combined as appropriate to form other embodiments that will be apparent to those skilled in the art. Such other embodiments are also within the scope of the present invention.|[0035] Unless defined otherwise, technical terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which the present application pertains, and the use of related terms herein is intended only to describe specific embodiments, not to limit the present application.|[0036] Unless otherwise indicated herein, reagents, instruments, equipment, and the like used in the present invention are those conventionally used by those skilled in the art.|[0037] Example 1|[0038] S1, fully soaking 10g of dried straw in 25g of mixed alkaline aqueous solution (pH 9) containing 5g/L of titanium dioxide and 1mmol/L of ruthenium chloride, then placing the straw in a freeze dryer, carrying out freeze drying at a medium speed of-60 ℃ and crushing to 8mm in size, reacting for 2h at 600 ℃ in a nitrogen atmosphere, preserving heat for 2h, and fully carbonizing to form the bimetal modified straw derived carbon material powder.|[0039] S2, adding straw derived carbon material powder into the cement-based material, mixing, and uniformly adding solid dry ice accounting for 0.2% of the mass of the cement-based material during the mixing to form slurry, wherein the mass ratio of the straw derived carbon material powder to the cement-based material is 1:200, the water-gel ratio of the cement-based material is controlled to be 0.5, and the gel-sand ratio is controlled to be 1:3.|[0040] S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃, wherein at least 5 hours of illumination is carried out every day.|[0041] After 28d of standard curing, the flexural strength of the test specimen was 10.2MPa, and the compressive strength was 55MPa.|[0042] Example two|[0043] S1, fully soaking 10g of dried straw in 20g of mixed alkaline aqueous solution (pH 9) containing 10g/L of titanium dioxide and 2mmol/L of ruthenium chloride, then placing the straw in a freeze dryer, carrying out freeze drying at a medium speed of-50 ℃ and crushing to 8mm in size, reacting for 2h at 700 ℃ in nitrogen atmosphere, preserving heat for 2h, and fully carbonizing to form the bimetal modified straw derived carbon material powder.|[0044] S2, adding the straw-derived carbon material powder into the cement-based material, mixing, and uniformly adding solid dry ice accounting for 1.5% of the mass of the cement-based material during the mixing to form slurry, wherein the mass ratio of the straw-derived carbon material powder to the cement-based material is 1:150, the water-gel ratio of the cement-based material is controlled to be 0.5, and the gel-sand ratio is controlled to be 1:3.|[0045] S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃, wherein at least 6 hours of illumination is carried out every day.|[0046] After 28d of standard curing, the flexural strength of the test specimen was 13.2MPa, and the compressive strength was 68MPa.|[0047] Example III|[0048] S1, fully soaking 10g of dried straw in 25g of mixed alkaline aqueous solution (pH of 10) containing 15g/L of titanium dioxide and 1.5mmol/L of ruthenium chloride, then placing the straw in a freeze dryer, carrying out freeze drying at a medium speed of-35 ℃ and crushing to 6mm in size, reacting for 1h at 800 ℃ in a nitrogen atmosphere, preserving heat for 2h, and fully carbonizing to form the bimetal modified straw derived carbon material powder.|[0049] S2, adding the straw-derived carbon material powder into the cement-based material, mixing, and uniformly adding solid dry ice accounting for 2% of the mass of the cement-based material during the mixing to form slurry, wherein the mass ratio of the straw-derived carbon material powder to the cement-based material is 1:150, the water-gel ratio of the cement-based material is controlled to be 0.5, and the gel-sand ratio is controlled to be 1:3.|[0050] S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃, wherein at least 6 hours of illumination is carried out every day.|[0051] After 28d of standard curing, the flexural strength of the test specimen was 12.3MPa, and the compressive strength was 62MPa.|[0052] Comparative example|[0053] The comparative example used the same cement-based material as in example one, without adding straw-derived carbon material powder and without adding solid dry ice during mixing, the slurry was poured into a standard mold, demolded after 24 hours, and cured in an environment with a relative humidity of 20±2 ℃ of 95% or more.|[0054] After 28d of standard curing, the flexural strength of the test specimen was 8MPa and the compressive strength was 40MPa.|[0055] The samples cured in examples one to three and comparative example were designated B1, B2, B3 and C1, respectively, and carbonization calculation was performed, and included the following steps:|[0056] (1) As shown in FIG. 1, the cement-based material during the maintenance was crushed into a sample a having a particle size of 1cm to 3cm, and the sample a was broken along the middle using a press and the exposed face was selected for calculation of the degree of carbonization. |[0057] (2) The section of sample a was cleaned slightly using a brush until the dust on the section of sample was cleaned.|[0058] (3) A1% phenolphthalein solution is selected as an indicator to spray on the cleaned cross section, the carbonized region b on the cross section is gray, and the non-carbonized region c is pink.|[0059] (4) The method comprises the steps of measuring the particle size Di of a sample and the particle size Di of a dye along any central line of a section of the sample a, recording the measured value of a first axis 1-1 as D1-D1, selecting a second axis 2-2, a third axis 3-3 and a fourth axis 4-4 along the selected first axis 1-1 at intervals of 45 degrees, measuring the particle size Di of the sample and the particle size Di of the dye on corresponding axes, and recording the D2-D2, the D3-D3 and the D4-D4 in sequence.|[0060] (5) The degree of carbonization in the different directions was calculated as (Di-Di)/Di or (Di 2-di2)/Di2, where i=1, 2,3,4. This was taken as the result of calculation of the degree of carbonization.|[0061] The carbonization results of the samples B1, B2, B3 and C1 at 7 days, 14 days and 28 days of curing age are shown in fig. 2, and the results are shown in table 1 below:|[0062] table 1 sample carbonization degree calculated in terms of width and calculated in terms of area |[0063] |[0064] Therefore, the carbon fixation strengthening method and the carbonization calculation method of the cement-based material, disclosed by the invention, keep the contact area of the cement-based material and carbon dioxide by introducing the straw derivative material modified by titanium and ruthenium into the cement-based material, so that the cement-based material is subjected to carbon fixation by photocatalysis in natural use, the durability and carbonization performance of the cement-based material are improved, and meanwhile, the provided carbonization calculation method is simple to operate, and the carbonization precision of the cement-based material is effectively improved.|[0065] It should be noted that the above-mentioned embodiments are merely for illustrating the technical solution of the present invention and not for limiting the same, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solution of the present invention may be modified or substituted by the same, and the modified or substituted technical solution may not deviate from the spirit and scope of the technical solution of the present invention. (CN120349127)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of cement-based material preparation, in particular to a carbon fixation strengthening method of a cement-based material and a carbonization calculation method thereof.|BACKGROUND ART|[0002] With the increasing global warming problem, low-carbon, environment-friendly and sustainable development is a target for pursuit by various countries. The traditional building material industry, especially the cement industry, has high carbon emissions due to the combustion of fossil fuels and the decomposition of carbonate minerals to produce CO 2 during production. The carbon emission of the cement industry accounts for 6-7% of the global artificial emission and is a typical high carbon emission industry. The cement-based carbon fixation strengthening method mainly adopts a carbon fixation maintenance technology to absorb and solidify CO 2 in the using stage of cement, so that the carbon footprint of the cement in the whole life cycle is reduced. The method not only helps to reduce carbon emissions, but also improves the performance of the cement-based material.|[0003] Therefore, the exploration of the carbon fixation strengthening method and the carbonization calculation method of the cement-based material is of great significance for realizing low carbonization and green of the field of building materials.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a carbon fixation strengthening method of a cement-based material and a carbonization calculation method thereof, wherein a titanium and ruthenium modified straw derivative material is introduced into the cement-based material, so that the contact area of the cement-based material and carbon dioxide is maintained, the cement-based material is subjected to carbon fixation by photocatalysis in natural use, the durability and carbonization performance of the cement-based material are improved, and meanwhile, the provided carbonization calculation method is simple to operate, and the accuracy of evaluating the carbonization of the cement-based material is effectively improved.|[0005] In order to achieve the above object, the present invention provides a carbon sequestration strengthening method for cement-based materials, comprising the steps of:|[0006] S1, fully soaking the dried straw in a mixed alkaline aqueous solution containing titanium dioxide and ruthenium chloride, then placing the straw in a freeze dryer for quick freeze drying and crushing, and fully carbonizing the straw in a nitrogen atmosphere to form bimetal modified straw derived carbon material powder; |[0007] s2, adding straw derived carbon material powder into a cement-based material, uniformly mixing to form slurry, controlling the water-glue ratio to be fixed at 0.4-0.6, and controlling the glue-sand ratio to be 1 (2-4); |[0008] S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃. |[0009] Preferably, in the step S1, the molar concentration of ruthenium chloride in the mixed alkaline aqueous solution is 1-2 mmol/L, the volume concentration of titanium dioxide is 5-20 g/L, the weight ratio of straw in the mixed aqueous solution is 1 (2-2.5), and the pH of the mixed alkaline aqueous solution is 9-10.|[0010] Preferably, in the step S1, the soaking time of the straw in the mixed aqueous solution is 2-8 hours, the temperature of a freeze dryer is minus 60-minus 20 ℃, the size after crushing is smaller than 10mm, the carbonization temperature is 500-800 ℃, the time is 2-6 hours, and the heat preservation is carried out for 2 hours.|[0011] Preferably, in the step S2, the mass ratio of the straw-derived carbon material powder to the cement-based material is 1 (50-200).|[0012] Preferably, in the step S2, solid dry ice is uniformly added in the mixing process of the straw derived carbon material powder and the cement-based material, and the mass ratio of the solid dry ice to the cement-based material is (0.2-3): 100.|[0013] Preferably, in step S3, at least 5 hours of light is irradiated daily during the curing process.|[0014] The invention also provides a cement-based material prepared by the method.|[0015] The invention also provides a carbonization calculation method of the cement-based material, which comprises the following steps:|[0016] (1) Crushing the cement-based material after curing for 28d into a sample with the particle size of 1cm-3cm, and using a press to break the sample along the middle and select the exposed surface for calculating the carbonization degree; |[0017] (2) Cleaning dust generated by breaking the sample on the exposed surface by using a powerful blower; |[0018] (3) Selecting phenolphthalein solution as an indicator to be sprayed on the cleaned sample section; |[0019] (4) Measuring the particle size of the sample and the width of the color development area along the center line of the section of the sample, and measuring the particle size of the artificial aggregate and the width of the color development area along the center lines in different directions again; |[0020] (5) The degree of carbonization of the samples was evaluated. |[0021] Preferably, in the step (5), the evaluation method is that the average value of the particle diameters of the samples in different directions on the average value ratio of the widths of the non-color-developing areas on different central lines is calculated, or the square of the average value of the particle diameters of the artificial aggregates on the average value ratio of the areas of the non-color-developing areas is calculated.|[0022] Therefore, the carbon fixation strengthening method and the carbonization calculation method of the cement-based material have the following beneficial effects:|[0023] (1) According to the invention, the straw derivative material is introduced into the cement-based material, so that the advantage of the void structure of the straw is maintained, and the pore canal which is favorable for carbon dioxide transmission is formed in the cement matrix, so that the contact area, carbonization depth and area of the cement-based material and carbon dioxide can be effectively increased, and the carbonization performance and durability of the material are improved. |[0024] (2) According to the invention, titanium dioxide is introduced into the straw derivative material, and photocatalysis carbon fixation is used for a long time in the cement-based material, so that the method has the remarkable energy-saving advantage, is convenient to implement, widens the natural carbon fixation process, ensures the dispersion of the titanium dioxide, and improves the abundance of active sites of the straw derivative material.|[0025] (3) The invention provides a carbonization calculation method of cement-based materials, which is simple to operate, and can quantitatively measure the carbonization degree of the cement-based materials in different curing stages, thereby effectively improving the accuracy of evaluating the carbonization of the cement-based materials.|[0026] The technical scheme of the invention is further described in detail through the drawings and the embodiments.|DRAWINGS DESCRIPTION|[0027] FIG. 1is a schematic diagram showing the results of a method for calculating carbonization of a cement-based material after carbon sequestration reinforcement according to an embodiment of the present invention;|[0028] FIG. 2 shows carbonization results of the inventive examples one-three and the comparative examples at 7 days, 14 days, and 28 days of curing age; |[0029] reference numerals |[0030] A. Sample, carbonized area, C, non-carbonized area, 1-1, first axis, 2-2, second axis, 3-3, third axis, 4-4, fourth axis, di, sample particle size, di, dyeing particle size.|INVENTION MODE|Detailed Description|[0031] The technical scheme of the invention is further described below through the attached drawings and the embodiments.|[0032] The technical scheme of the invention is further described below through the attached drawings and the embodiments.|[0033] Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs.|[0034] Furthermore, it should be understood that although the present disclosure describes embodiments, not every embodiment is provided with a separate embodiment, and that this description is provided for clarity only, and that the disclosure is not limited to the embodiments described in detail below, and that the embodiments described in the examples may be combined as appropriate to form other embodiments that will be apparent to those skilled in the art. Such other embodiments are also within the scope of the present invention.|[0035] Unless defined otherwise, technical terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which the present application pertains, and the use of related terms herein is intended only to describe specific embodiments, not to limit the present application.|[0036] Unless otherwise indicated herein, reagents, instruments, equipment, and the like used in the present invention are those conventionally used by those skilled in the art.|[0037] Example 1|[0038] S1, fully soaking 10g of dried straw in 25g of mixed alkaline aqueous solution (pH 9) containing 5g/L of titanium dioxide and 1mmol/L of ruthenium chloride, then placing the straw in a freeze dryer, carrying out freeze drying at a medium speed of-60 ℃ and crushing to 8mm in size, reacting for 2h at 600 ℃ in a nitrogen atmosphere, preserving heat for 2h, and fully carbonizing to form the bimetal modified straw derived carbon material powder.|[0039] S2, adding straw derived carbon material powder into the cement-based material, mixing, and uniformly adding solid dry ice accounting for 0.2% of the mass of the cement-based material during the mixing to form slurry, wherein the mass ratio of the straw derived carbon material powder to the cement-based material is 1:200, the water-gel ratio of the cement-based material is controlled to be 0.5, and the gel-sand ratio is controlled to be 1:3.|[0040] S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃, wherein at least 5 hours of illumination is carried out every day.|[0041] After 28d of standard curing, the flexural strength of the test specimen was 10.2MPa, and the compressive strength was 55MPa.|[0042] Example two|[0043] S1, fully soaking 10g of dried straw in 20g of mixed alkaline aqueous solution (pH 9) containing 10g/L of titanium dioxide and 2mmol/L of ruthenium chloride, then placing the straw in a freeze dryer, carrying out freeze drying at a medium speed of-50 ℃ and crushing to 8mm in size, reacting for 2h at 700 ℃ in nitrogen atmosphere, preserving heat for 2h, and fully carbonizing to form the bimetal modified straw derived carbon material powder.|[0044] S2, adding the straw-derived carbon material powder into the cement-based material, mixing, and uniformly adding solid dry ice accounting for 1.5% of the mass of the cement-based material during the mixing to form slurry, wherein the mass ratio of the straw-derived carbon material powder to the cement-based material is 1:150, the water-gel ratio of the cement-based material is controlled to be 0.5, and the gel-sand ratio is controlled to be 1:3.|[0045] S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃, wherein at least 6 hours of illumination is carried out every day.|[0046] After 28d of standard curing, the flexural strength of the test specimen was 13.2MPa, and the compressive strength was 68MPa.|[0047] Example III|[0048] S1, fully soaking 10g of dried straw in 25g of mixed alkaline aqueous solution (pH of 10) containing 15g/L of titanium dioxide and 1.5mmol/L of ruthenium chloride, then placing the straw in a freeze dryer, carrying out freeze drying at a medium speed of-35 ℃ and crushing to 6mm in size, reacting for 1h at 800 ℃ in a nitrogen atmosphere, preserving heat for 2h, and fully carbonizing to form the bimetal modified straw derived carbon material powder.|[0049] S2, adding the straw-derived carbon material powder into the cement-based material, mixing, and uniformly adding solid dry ice accounting for 2% of the mass of the cement-based material during the mixing to form slurry, wherein the mass ratio of the straw-derived carbon material powder to the cement-based material is 1:150, the water-gel ratio of the cement-based material is controlled to be 0.5, and the gel-sand ratio is controlled to be 1:3.|[0050] S3, pouring the slurry into a standard mold, demolding after 24 hours, and curing in an environment with the relative humidity of more than 95% at 20+/-2 ℃, wherein at least 6 hours of illumination is carried out every day.|[0051] After 28d of standard curing, the flexural strength of the test specimen was 12.3MPa, and the compressive strength was 62MPa.|[0052] Comparative example|[0053] The comparative example used the same cement-based material as in example one, without adding straw-derived carbon material powder and without adding solid dry ice during mixing, the slurry was poured into a standard mold, demolded after 24 hours, and cured in an environment with a relative humidity of 20±2 ℃ of 95% or more.|[0054] After 28d of standard curing, the flexural strength of the test specimen was 8MPa and the compressive strength was 40MPa.|[0055] The samples cured in examples one to three and comparative example were designated B1, B2, B3 and C1, respectively, and carbonization calculation was performed, and included the following steps:|[0056] (1) As shown in FIG. 1, the cement-based material during the maintenance was crushed into a sample a having a particle size of 1cm to 3cm, and the sample a was broken along the middle using a press and the exposed face was selected for calculation of the degree of carbonization. |[0057] (2) The section of sample a was cleaned slightly using a brush until the dust on the section of sample was cleaned.|[0058] (3) A1% phenolphthalein solution is selected as an indicator to spray on the cleaned cross section, the carbonized region b on the cross section is gray, and the non-carbonized region c is pink.|[0059] (4) The method comprises the steps of measuring the particle size Di of a sample and the particle size Di of a dye along any central line of a section of the sample a, recording the measured value of a first axis 1-1 as D1-D1, selecting a second axis 2-2, a third axis 3-3 and a fourth axis 4-4 along the selected first axis 1-1 at intervals of 45 degrees, measuring the particle size Di of the sample and the particle size Di of the dye on corresponding axes, and recording the D2-D2, the D3-D3 and the D4-D4 in sequence.|[0060] (5) The degree of carbonization in the different directions was calculated as (Di-Di)/Di or (Di 2-di2)/Di2, where i=1, 2,3,4. This was taken as the result of calculation of the degree of carbonization.|[0061] The carbonization results of the samples B1, B2, B3 and C1 at 7 days, 14 days and 28 days of curing age are shown in fig. 2, and the results are shown in table 1 below:|[0062] table 1 sample carbonization degree calculated in terms of width and calculated in terms of area |[0063] |[0064] Therefore, the carbon fixation strengthening method and the carbonization calculation method of the cement-based material, disclosed by the invention, keep the contact area of the cement-based material and carbon dioxide by introducing the straw derivative material modified by titanium and ruthenium into the cement-based material, so that the cement-based material is subjected to carbon fixation by photocatalysis in natural use, the durability and carbonization performance of the cement-based material are improved, and meanwhile, the provided carbonization calculation method is simple to operate, and the carbonization precision of the cement-based material is effectively improved.|[0065] It should be noted that the above-mentioned embodiments are merely for illustrating the technical solution of the present invention and not for limiting the same, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solution of the present invention may be modified or substituted by the same, and the modified or substituted technical solution may not deviate from the spirit and scope of the technical solution of the present invention. Family Number|(115363993)|115363993|Abstract|(CN120349127 A)|The invention discloses a carbon sequestration strengthening method of a cement - based material and a carbonization calculation method of the cement - based material , and belongs to the technical field of cement - based material preparation . The preparation method comprises the following steps : fully soaking dried straws in a mixed alkaline aqueous solution containing titanium dioxide and ruthenium chloride , putting the straws in a freeze dryer for quick - freezing , drying and crushing , and fully carbonizing in a nitrogen atmosphere to form bimetallic modified straw derived carbon material powder ; adding the straw derived carbon material powder into a cement - based material , and uniformly mixing to form slurry ; and pouring the slurry into a standard mold for curing . The titanium and ruthenium modified straw derivative material is introduced into the cement - based material , the contact area of the cement - based material and carbon dioxide is kept , carbon sequestration is conducted on the cement - based material through photocatalysis in the natural use process , the durability and carbonization performance of the cement - based material can be improved , and meanwhile the provided carbonization calculation method is easy to operate and low in cost . And the precision of evaluating the carbonization of the cement - based material is effectively improved . |CPC codes|(CN120349127 A)|C01B - 032/05 |IPC codes|(CN120349127 A)|C01B - 032/05 |Title|(CN120349127 A)|Carbon sequestration strengthening method and carbonization calculation method of cement - based material | Materials, metallurgy C01B-032/05|C04B-014/02|C04B-014/02/2|C04B-014/02/4|C04B-014/06|C04B-014/06/2|C04B-014/06/8|C04B-014/10/4|C04B-014/10/6|C04B-014/38/6|C04B-018/08|C04B-018/14/6|C04B-018/16|C04B-018/24|C04B-024/24|C04B-028/00|C04B-028/04|C04B-038/02|C04B-040/00/82|C04B-040/02|C04B-040/02/31|C04B-040/02/4|C04B-040/02/59|C04B-040/02/63|C04B-2103/0001|C04B-2103/302|C04B-2111/00017|C04B-2111/40|C04B-2201/32|C04B-2201/50 C01B-032/05|C04B-014/02|C04B-014/02/2|C04B-014/02/4|C04B-014/06|C04B-014/06/2|C04B-014/06/8|C04B-014/10/4|C04B-014/10/6|C04B-014/38/6|C04B-018/08|C04B-018/14/6|C04B-018/16|C04B-018/24|C04B-024/24|C04B-028/00|C04B-028/04|C04B-038/02|C04B-040/00/82|C04B-040/02|C04B-040/02/31|C04B-040/02/4|C04B-040/02/59|C04B-040/02/63|C04B-2103/0001|C04B-2103/302|C04B-2111/00017|C04B-2111/40|C04B-2201/32|C04B-2201/50 C01B-032/05|C04B-014/36|C04B-028/00|C04B-040/02 C01B-032/05|C04B-014/36|C04B-028/00|C04B-040/02 PENDING (CN120349127)|PENDING ALIVE (CN120349127)|ALIVE (CN120349127)|LEGAL DETAILS FOR CN120349127|Actual or expected expiration date=2045-05-08|Legal state=ALIVE|Status=PENDING|Event publication date=2025-05-08|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510587920|Application date=2025-05-08|Standardized application number=2025CN-0587920|Event publication date=2025-07-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120349127|Publication stage code=A|Publication date=2025-07-22|Standardized publication number=CN120349127|Event publication date=2025-07-22|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-08-08|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN120349127)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKeZD0GUGkPC1Ffn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000078271384&ekey=2359&xpn=CN120349127&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=m53pR1TGmfdVVBIQ6vlBoJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN120349127)|CN (CN120349127)|NAME=SHENZHEN UNIVERSITY , COUNTRY=CN (CN120349127)|NAME=ZHAO RONG;BEIJING ZHIYI INTERNET INTELLECTUAL PROPERTY AGENCY CO., LTD , REG=16137 (CN120349127)|NAME=LIU JUN|NAME=ZHENG WENTAO|NAME=ZHANG WEIZHUO|NAME=CHENG LEI|NAME=OU GUANGMING 0 1 Titre: (CN120349127)|Carbon sequestration strengthening method and carbonization calculation method of cement-based material Résumé: (CN120349127)|The invention discloses a carbon sequestration strengthening method of a cement-based material and a carbonization calculation method of the cement-based material, and belongs to the technical field of cement-based material preparation. The preparation method comprises the following steps: fully soaking dried straws in a mixed alkaline aqueous solution containing titanium dioxide and ruthenium chloride, putting the straws in a freeze dryer for quick-freezing, drying and crushing, and fully carbonizing in a nitrogen atmosphere to form bimetallic modified straw derived carbon material powder; adding the straw derived carbon material powder into a cement-based material, and uniformly mixing to form slurry; and pouring the slurry into a standard mold for curing. The titanium and ruthenium modified straw derivative material is introduced into the cement-based material, the contact area of the cement-based material and carbon dioxide is kept, carbon sequestration is conducted on the cement-based material through photocatalysis in the natural use process, the durability and carbonization performance of the cement-based material can be improved, and meanwhile the provided carbonization calculation method is easy to operate and low in cost. And the precision of evaluating the carbonization of the cement-based material is effectively improved. 28 Abstract gpt-4o-mini no The article focuses on carbon sequestration in cement-based materials, which is not related to the accelerated weathering of silicate or alkaline minerals for CO₂ capture.
30 CN202511396598 CN202511396598 CN121286156 117384248 CN121286156 A 2026-01-09 [CN121286156] 2025-09-28 2025-09-28 2026-01-09 (CN121286156)|2045-09-28 (CN121286156)|Method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment (CN121286156)|The invention provides a method for improving the carbon sequestration and emission reduction capacity of acid soil based on straw treatment, and relates to the field of soil improvement technologies and low-carbon production, and the method comprises the three steps of straw preparation and differential treatment, field returning material preparation and application, and monitoring and regulation after application. According to the invention, differential crushing treatment and differential stack retting treatment are carried out according to the characteristics of straw materials, so that the straw treatment link is optimized, the decomposition period is shortened, the quality uniformity of returning materials is ensured, the problem of incomplete decomposition or nutrient loss caused by material difference is solved, and a low-cost material compounding mode is adopted, so that the quality of the returning materials is improved. The agricultural waste peanut shells are used for preparing the biochar, then the industrial byproduct desulfurized gypsum is used for replacing commercial gypsum, the material preparation cost is reduced, then through cooperation of the decomposed straw and the biochar, the accumulation amount and stability of soil organic carbon are improved, and the effect of improving the carbon sequestration and emission reduction capacity of the acid soil is achieved. GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES INSTITUTE OF AGRICULTURAL RESOURCES & ENVIRONMENT (CN121286156)|GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES, INSTITUTE OF AGRICULTURAL RESOURCES AND ENVIRONMENT ([CN]) HUANG QIAOYI|TANG SHUANHU|WU TENGFEI|HUANG JIANFENG|HUANG XU|ZHANG MU|YI QIONG|PANG YUWAN|DING WUHAN|CENG KE|LI PING|FU HONGTING|WU YONGPEI|LUO HAIBIN (CN121286156)|HUANG QIAOYI|TANG SHUANHU|WU TENGFEI|HUANG JIANFENG|HUANG XU|ZHANG MU|YI QIONG|PANG YUWAN|DING WUHAN|CENG KE|LI PING|FU HONGTING|WU YONGPEI|LUO HAIBIN (CN121286156)|SUN JIAN;BEIJING SHENGGUANGXINHE IP FIRM|Reg. Nb: 16117 (CN121286156)|The method has the beneficial effects that differential crushing treatment and differential stack retting treatment are carried out according to the characteristics of straw materials, so that the straw treatment link is optimized, the decomposition period is shortened, the quality uniformity of returning materials is ensured, the problems of incomplete decomposition or nutrient loss caused by material difference are solved, the biochar is prepared by utilizing agricultural waste peanut shells in a low-cost material compounding manner, industrial byproduct desulfurized gypsum is used for replacing commodity gypsum, the cost of preparing materials is reduced, and the accumulation amount and stability of organic carbon in soil are improved through the synergistic cooperation of the decomposed straw and the biochar, so that the effect of improving the carbon fixation and emission reduction capability of acid soil is achieved.|The method is further improved in that in the first step, the judging standard of the decomposed straw is that the decomposition is judged to be completed when the temperature of the pile body is reduced to below 30 ℃, the color of the pile body is changed to dark brown, the pile body is fragile by hand pinching, the pile body has no acid odor, and the pH value of the pile body is stabilized at 6.0-7.0.| (CN121286156)|1. The method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment is characterized by comprising the following steps of: Step one, preparing straw and performing differentiation treatment Preparing straw materials, carrying out differential crushing treatment according to the characteristics of the straw materials to obtain crushed straw, mixing the crushed straw with livestock manure according to a mass ratio of 8:2, adding lime in an amount of 2-3% of the weight of the crushed straw in the mixing process, adjusting the pH value of the mixed material to 6.0-6.5 to obtain a quenched and tempered mixed material, and carrying out differential composting treatment on the quenched and tempered mixed material to obtain decomposed straw; Step two, preparation and application of Tian Wuliao Preparing a compounded functional material and a compound microbial agent, wherein the functional material comprises biochar and desulfurized gypsum, the compound microbial agent is a compound microbial agent containing azotobacter and phosphate-dissolving bacteria, then the functional material and the compound microbial agent are mixed with decomposed straws to obtain Tian Wuliao, and then the returning material is uniformly spread in a target area in which soil needs to be improved according to the use amount of 4.5-8 tons per hectare; step three, monitoring and controlling after application After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result.| (CN121286156)|In view of the above problems, the present invention aims to provide a method for improving the carbon sequestration and emission reduction capacity of acidic soil based on straw treatment, which improves the accumulation of organic carbon in the soil, not only improves the soil fertility, but also reduces the carbon dioxide concentration in the atmosphere through the carbon fixation effect and relieves the greenhouse gas effect.The invention aims at realizing the aim by adopting the following technical scheme that the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment comprises the following steps:|The invention provides a method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment, which relates to the fields of soil improvement technology and low-carbon production, and comprises three steps of preparing straw and differential treatment, preparing Tian Wuliao and applying and monitoring and regulating after applying, the invention carries out differential crushing treatment and differential composting treatment aiming at straw material characteristics, optimizes straw treatment links, shortens the decomposition period, ensures the quality uniformity of returning materials, the problems of incomplete decomposition or nutrient loss caused by material difference are solved, the biochar is prepared by adopting a low-cost material compounding mode and utilizing agricultural waste peanut shells, industrial byproduct desulfurized gypsum replaces commodity gypsum, and the cost of the prepared materials is reduced.|The invention relates to the field of soil improvement technology and low-carbon production, in particular to a method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment.| (CN121286156)|ACID SOIL(100,21)|CARBON SEQUESTRATION(100,18)|STRAW TREATMENT(100,17)|EMISSION REDUCTION CAPACITY(100,15)|DECOMPOSED STRAW SYNERGISTIC COOPERATION(98,1)|STRAW DECOMPOSITION(96,42)|AGRICULTURAL WASTE PEANUT SHELL(86,2)|CRUSHED STRAW(71,9)|REPLACING COMMODITY GYPSUM(70,1)|DIFFERENTIAL COMPOSTING TREATMENT(68,3)|COMMODITY GYPSUM(67,1)|STRAW TREATMENT LINK(62,2)|DECOMPOSING STRAW CRITERION(58,1)|INCOMPLETE DECOMPOSITION(54,6)|DECOMPOSED STRAW MASS(51,15)|QUALITY UNIFORMITY(51,2)|SYNERGISTIC COOPERATION(51,1)|DIFFERENTIAL CRUSHING TREATMENT(49,6)|BYPRODUCT(47,2)|PILE COLOR(47,2)|DECOMPOSED STRAW DOSAGE(44,11)|BIOCHAR(41,16)|WHEAT STRAW(40,22)|PHOSPHATE DISSOLVING BACTERIUM(35,12)|DECOMPOSITION PERIOD(35,3)|DIFFERENTIAL TREATMENT(34,1)|NUTRIENT LOSS(33,6)|PILE(32,16)|CRUSHED STRAW WEIGHT(31,5)|PILE TEMPERATURE(31,2)|BIOCHAR DOSAGE(30,5)|AUTUMN HARVEST(28,5)|SOIL IMPROVEMENT(28,2)|GYPSUM(27,17)|DIFFERENTIATION TREATMENT(26,5)|HAND PINCHING(25,2)|RETURNING MATERIAL QUALITY UNIFORMITY(25,2)|STRAW MATERIAL(24,10)|DIFFERENTIAL STACK(23,7)|JUDGING(23,1)|EMISSION VALUE(22,14)|SOIL MICROORGANISM MINERALIZATION(22,3)|LIVESTOCK(22,2)|HECTARE(21,16)|ACIDIC SOIL(21,2)|GROUND(20,16)|STRAW(20,12)|DECOMPOSITION(20,11)|LIME ADDITION(20,5)|TEMPERED MIXED MATERIAL(20,4)|BAGASSE(19,19)|RICE STRAW(19,19)|PH VALUE(19,17)|AZOTOBACTER(19,12)|SOUR ODOR(19,1)|CORN STRAW(18,25)|GROUND LAYER(18,8)|REGULATION(18,5)|RETURNING MATERIAL(17,29)|PHOSPHATE DISSOLVING BACTERIUM DOSAGE(17,3)|SOIL FERTILITY(17,3)|MATERIAL COMPOUND(17,1)|CARBON FIXATION(16,5)|REGULATION TREATMENT MODE(16,4)|ORGANIC CARBON STABILITY(16,1)|TON(15,19)|DARK BROWN(15,5)|EMISSION REDUCTION CAPABILITY(15,2)|ACIDIC SOIL EMISSION REDUCTION(15,1)|CARBON DIOXIDE(15,1)|SOIL DENITRIFICATION(14,3)|MATERIAL DIFFERENCE(14,2)|HALF YEAR(13,5)|RAINY SEASON(13,5)|GREENHOUSE GAS(13,2)|SOIL IMPROVEMENT FIELD(13,2)|COMPOSTING PERIOD(12,9)|DISSOLVABLE PHOSPHORUS(12,3)|LIVESTOCK MANURE(12,3)|MAKING MATERIAL(12,1)|DECOMPOSITION MODERATION(10,3)|ENOUGH MICROORGANISM ADHESION(10,3)|MOISTURE PRESERVATION(10,3)|COMPOUND FUNCTIONAL MATERIAL(10,2)|FARMLAND SOIL(10,2)|LOW CARBON PRODUCTION(10,2)|PREPARING MATERIAL COST(10,1)|STRAW INCOMPLETE DECOMPOSITION(10,1)|RETURNING MATERIAL CONSUMPTION(9,8)|ORGANIC CARBON(9,6)|MIXED MATERIAL(9,2)|COMPOUND MICROBIAL INOCULANT(8,3)|DIFFERENTIAL CRUSHING(8,3)|EARLY DECAY(8,3)|FIBER TOUGHNESS(8,3)|HUMID ENVIRONMENT(8,3)|OXYGEN SUPPLEMENTATION(8,3)|SLOW PYROLYSIS(8,3)|STRAW STABILITY(8,3)|COMPOSTING(7,15)|MIXING(7,8)|BACILLUS(7,6)|CONTROL TREATMENT(7,6)|DECOMPOSITION SPEED(7,6)|PSEUDOMONAS(7,6)|DETECTION RESULT(7,5)|DIFFERENTIAL STACK MODE(7,3)|DRIED STRAW(7,3)|LIGNIN CONTENT(7,3)|MULCHING FILM(7,3)|SMASH(7,3)|STACK HEIGHT(7,3)|TEMPERING(7,3)|UNIFORM DECOMPOSITION(7,3)|TARGET AREA(6,13)|NEXT PRODUCTION SEASON(6,9)|MASS RATIO(6,5)|FORESTRY WASTE(6,1)|VALUABLE RESOURCE(6,1)|AZOSPIRILLUM(5,3)|COW MANURE(5,3)|HEAT RADIATION(5,3)|LIGNIFICATION DEGREE(5,3)|NEUTRALIZING ORGANIC ACID(5,3)|OVERHIGH(5,3)|OVERLONG(5,3)|PORTABLE GAS CHROMATOGRAPH(5,3)|RETTING(5,3)|VENTILATION(5,3)|VIRTUOUS CIRCLE(5,3)|ALKALINE SUBSTANCE(5,2)|CADMIUM CONTENT(5,2)|WASTE TREATMENT(5,2)|AGRICULTURE GREEN PRODUCTION(5,1)| (CN121286156)|1. The method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment is characterized by comprising the following steps of:| Step one, preparing straw and performing differentiation treatment |Preparing straw materials, carrying out differential crushing treatment according to the characteristics of the straw materials to obtain crushed straw, mixing the crushed straw with livestock manure according to a mass ratio of 8:2, adding lime in an amount of 2-3% of the weight of the crushed straw in the mixing process, adjusting the pH value of the mixed material to 6.0-6.5 to obtain a quenched and tempered mixed material, and carrying out differential composting treatment on the quenched and tempered mixed material to obtain decomposed straw;| Step two, preparation and application of Tian Wuliao |Preparing a compounded functional material and a compound microbial agent, wherein the functional material comprises biochar and desulfurized gypsum, the compound microbial agent is a compound microbial agent containing azotobacter and phosphate-dissolving bacteria, then the functional material and the compound microbial agent are mixed with decomposed straws to obtain Tian Wuliao, and then the returning material is uniformly spread in a target area in which soil needs to be improved according to the use amount of 4.5-8 tons per hectare;| step three, monitoring and controlling after application |After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result.|2. The method for improving carbon sequestration and emission reduction of acidic soil based on straw treatment according to claim 1, wherein in the first step, the straw material is one of rice straw, corn straw, wheat straw and bagasse, wherein the rice straw and the bagasse are crushed to 3-5 cm, and the corn straw and the wheat straw are crushed to 2-4 cm.|3. The method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment according to claim 1, wherein in the first step, the criterion of decomposing straw is that decomposition is judged to be completed when the temperature of a pile is reduced to below 30 ℃, the color of the pile becomes dark brown, the pile is fragile by hand pinching, no acid odor exists, and the pH value is stabilized at 6.0-7.0.|4. The method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment according to claim 1, wherein in the second step, biochar is prepared by carrying out low-speed pyrolysis on peanut shells at 300-500 ℃ for 2-4 hours, and the grain size is 2-5 mm, and the dosage of the biochar is 60-100% of the mass of decomposed straw.|5. The method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment according to claim 1, wherein in the second step, the content of heavy metals lead and cadmium in the desulfurized gypsum is lower than 100mg/kg, and the dosage is 40-60% of the mass of decomposed straw.|6. The method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment according to claim 1, wherein in the second step, the amount of the composite microbial agent is 0.2-0.4% of the mass of decomposed straw.|7. The method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment according to claim 1, wherein in the third step, the pH value is measured once every half year, and the CO 2 emission value and the N 2 O emission value are measured after rainy season and autumn harvest.|8. The method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment according to claim 1, wherein in the third step, the specific mode of the regulation treatment is as follows:| when the pH value is less than 5.5, the consumption of returning materials is increased by 1-2 tons per hectare; | When the CO 2 emission value is more than 500 mg/(m 2.h), the dosage of decomposed straw in the returning materials is reduced by 10 percent; | When the emission value of N 2 O is more than 10 mug/(m 2 h), the dosage of the composite microbial agent in the returning materials is increased by 5%. (CN121286156)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the field of soil improvement technology and low-carbon production, in particular to a method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment.|BACKGROUND ART|[0002] With the increasing global climate change problem, farmland greenhouse gas emissions (especially methane and nitrous oxide) are attracting more and more attention. In agricultural production activities, especially soil management and crop production, are one of the important sources of greenhouse gas emissions. However, most cultivated lands in China have the problem of acidification, a large amount of farmland soil belongs to acid soil (pH value is less than 5.5), and the farmland soil usually lacks alkaline mineral elements such as calcium, magnesium and the like, which are critical to the growth of crops, and meanwhile, many beneficial soil microorganisms (such as azotobacter, phosphate-dissolving bacteria and the like) have lower activity in the acid soil, so that the soil fertility is insufficient, the emission of greenhouse gases is high, and the growth of crops and the green production of agriculture are limited.|[0003] Therefore, the improvement of acid soil and carbon sequestration and emission reduction are always one of important research directions in the agricultural field. In the prior art, the improvement of acid soil mainly depends on the neutralization by using alkaline substances such as lime, serpentine and the like, and the improvement of soil structure by returning organic substances (such as straw, agricultural and forestry waste and the like) to fields, thereby improving soil fertility and carbon reserves. For the traditional improvement mode of returning the straws to the field, the decomposition period is longer, the influence of the climatic conditions is larger, the incomplete decomposition of the straws, the loss of nutrients and the increase of greenhouse gas emission are easily caused, and the long-term health of soil and the agricultural green production level are influenced, so the invention provides a method for improving the carbon sequestration and emission reduction capability of acid soil based on straw treatment to solve the problems in the prior art.|DISCLOSURE|Disclosure of Invention|[0004] In view of the above problems, the present invention aims to provide a method for improving the carbon sequestration and emission reduction capacity of acidic soil based on straw treatment, which improves the accumulation of organic carbon in the soil, not only improves the soil fertility, but also reduces the carbon dioxide concentration in the atmosphere through the carbon fixation effect and relieves the greenhouse gas effect.|[0005] The invention aims at realizing the aim by adopting the following technical scheme that the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment comprises the following steps:|[0006] Step one, preparing straw and performing differentiation treatment |[0007] Preparing straw materials, carrying out differential crushing treatment according to the characteristics of the straw materials to obtain crushed straw, mixing the crushed straw with livestock manure according to a mass ratio of 8:2, adding lime in an amount of 2-3% of the weight of the crushed straw in the mixing process, adjusting the pH value of the mixed material to 6.0-6.5 to obtain a quenched and tempered mixed material, and carrying out differential composting treatment on the quenched and tempered mixed material to obtain decomposed straw;|[0008] Step two, preparation and application of Tian Wuliao |[0009] Preparing a compounded functional material and a compound microbial agent, wherein the functional material comprises biochar and desulfurized gypsum, the compound microbial agent is a compound microbial agent containing azotobacter and phosphate-dissolving bacteria, then the functional material and the compound microbial agent are mixed with decomposed straws to obtain Tian Wuliao, and then the returning material is uniformly spread in a target area in which soil needs to be improved according to the use amount of 4.5-8 tons per hectare;|[0010] step three, monitoring and controlling after application |[0011] After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result.|[0012] The method is further improved in that in the first step, the straw material is one of rice straw, corn straw, wheat straw and bagasse, wherein the rice straw and the bagasse are crushed to 3-5 cm, and the corn straw and the wheat straw are crushed to 2-4 cm.|[0013] The method is further improved in that in the first step, the judging standard of the decomposed straw is that the decomposition is judged to be completed when the temperature of the pile body is reduced to below 30 ℃, the color of the pile body is changed to dark brown, the pile body is fragile by hand pinching, the pile body has no acid odor, and the pH value of the pile body is stabilized at 6.0-7.0.|[0014] The method is further improved in that in the second step, the biochar is prepared by carrying out slow pyrolysis on peanut shells for 2-4 hours at the temperature of 300-500 ℃, the particle size is 2-5 mm, and the dosage of the biochar is 60-100% of the mass of the decomposed straw.|[0015] The method is further improved in that in the second step, the content of heavy metals lead and cadmium in the desulfurized gypsum is lower than 100mg/kg, and the dosage of the heavy metals lead and cadmium in the desulfurized gypsum is 40-60% of the mass of the decomposed straw.|[0016] The method is further improved in that in the second step, the dosage of the composite microbial agent is 0.2-0.4% of the mass of the decomposed straw.|[0017] The further improvement is that in the third step, the pH value is measured every half year, and the CO 2 emission value and the N 2 O emission value are measured after rainy season and autumn harvest.|[0018] The method is further improved in that in the third step, the specific mode of regulation and control treatment is as follows:|[0019] when the pH value is less than 5.5, the consumption of returning materials is increased by 1-2 tons per hectare; |[0020] When the CO 2 emission value is more than 500 mg/(m 2.h), the dosage of decomposed straw in the returning materials is reduced by 10 percent; |[0021] When the emission value of N 2 O is more than 10 mug/(m 2 h), the dosage of the composite microbial agent in the returning materials is increased by 5%. |[0022] The method has the beneficial effects that differential crushing treatment and differential stack retting treatment are carried out according to the characteristics of straw materials, so that the straw treatment link is optimized, the decomposition period is shortened, the quality uniformity of returning materials is ensured, the problems of incomplete decomposition or nutrient loss caused by material difference are solved, the biochar is prepared by utilizing agricultural waste peanut shells in a low-cost material compounding manner, industrial byproduct desulfurized gypsum is used for replacing commodity gypsum, the cost of preparing materials is reduced, and the accumulation amount and stability of organic carbon in soil are improved through the synergistic cooperation of the decomposed straw and the biochar, so that the effect of improving the carbon fixation and emission reduction capability of acid soil is achieved.|DRAWINGS DESCRIPTION|[0023] FIG. 1 is a schematic flow chart of the steps of the present invention.|INVENTION MODE|Detailed Description|[0024] The present invention will be further described in detail with reference to the following examples, which are only for the purpose of illustrating the invention and are not to be construed as limiting the scope of the invention.|[0025] In the examples below, the sources of materials are all commercially available.|[0026] Example 1|[0027] According to the embodiment shown in fig. 1, the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment is provided, and comprises the following steps:|[0028] Step one, preparing straw and performing differentiation treatment |[0029] Suitable straw materials (rice straw, corn straw, wheat straw and bagasse) are selected, and differential crushing treatment is performed according to straw material characteristics (lignification degree and fiber structure), wherein the rice straw and the bagasse are crushed to 3cm, and the corn straw and the wheat straw are crushed to 2m. Specifically, for rice straw, the rice straw contains lower lignin, the fiber is softer and is easy to decompose, if the fiber is too thin (less than 2 cm), the fiber can cause early decay or loss in the composting process, if the fiber is too thick (more than 5 cm), the decomposition speed is slow, and the composting period is prolonged, so that the embodiment adopts a 3cm design, not only can ensure enough microorganism adhesion surface area, but also can prevent excessive smashing to cause excessive accumulation, poor air permeability or nutrient loss with water in a humid environment. For bagasse, the bagasse contains higher fibers and less lignin, has higher toughness, can ensure moderate decomposition speed by crushing to 3cm particle size, can better utilize microbial activity generated in the composting process, and keeps enough space for oxidation reaction. For corn straw and wheat straw, the lignin content is higher, the fiber toughness is strong, so that the contact area between the corn straw and microorganisms can be increased by crushing the corn straw and the wheat straw to 2cm, the decomposition is promoted, the decomposition speed is slow due to overhigh (more than 5 cm), and the difficulty in retting can be increased due to overlong (less than 2 cm). Therefore, the differential crushing can not only improve the decomposition efficiency, but also ensure the stability of the straws and the virtuous circle of the microbial activity in the composting process, and avoid the incomplete decomposition problem caused by different types of the straws.|[0030] And then mixing the mixture with livestock manure (cow manure) according to a mass ratio of 8:2, adding lime in an amount which is 2% of the weight of the crushed straw in the mixing process, and adjusting the pH value to be within a range of 6.0-6.5, thereby obtaining the tempering mixture after the mixing is completed. In the mixing process, lime is used for neutralizing organic acid in the pile body, and the pH value is regulated to be in the range of 6.0-6.5, so that the activity of microorganisms in the composting process is facilitated, and the ventilation and decomposition effects of the pile body are ensured.|[0031] Carrying out differential stack retting treatment on the quenched and tempered mixture to obtain decomposed straws, wherein the specific mode of the differential stack retting treatment is as follows:|[0032] For rice straw and bagasse, the stacking height is 1.0 meter, so that internal anaerobic caused by excessive stacking is prevented. The surface layer is covered with dried straw with the thickness of 5cm for moisture preservation and rain prevention. The composting period is 45 days. When the temperature of the center of the pile body is raised to 55 ℃ or above, turning the pile for 1 time in the whole period, namely turning once every 30 days, wherein the turning aims at radiating heat and cooling, supplementing oxygen, preventing the pile from being burned and promoting uniform decomposition; |[0033] For corn straw and wheat straw, the corn straw and wheat straw are piled up by 1.5 meters to reduce water evaporation, covered with a mulching film to preserve soil moisture, and piled up for 60 days in a composting period, water is sprayed 1 time every 15 days, so that the water content of the piled up body is kept within the range of 60% -65%, and the metabolic activity of microorganisms is ensured. |[0034] Monitoring the temperature, color, texture and smell of the piled body in the composting process, and judging that the thoroughly decomposed straw is obtained when the temperature of the piled body is reduced to below 30 ℃, the color of the piled body is changed into dark brown, the piled body is easy to pinch by hands, the piled body has no acid odor and the pH value of the piled body is stable within the range of 6.0-7.0.|[0035] Step two, preparation and application of Tian Wuliao|[0036] The functional materials comprise biochar and desulfurized gypsum, the biochar is specifically prepared by carrying out low-speed pyrolysis on peanut shells (local agricultural wastes) for 4 hours at the temperature of 300 ℃, the particle size is 2mm, the biochar has a good porous structure and is favorable for improving the physicochemical property of soil, the dosage of the biochar is 60% of the mass of decomposed straw, the desulfurized gypsum contains higher calcium element, the acidity of the soil can be effectively neutralized, the soil structure is improved, meanwhile, the heavy metal lead and cadmium contents of the desulfurized gypsum are all lower than 100mg/kg, the safety of the desulfurized gypsum is ensured, and the corresponding dosage is 40% of the mass of the decomposed straw.|[0037] For the microbial agent, a commercially available composite microbial agent is selected and contains effective azotobacter and phosphate-dissolving bacteria. Azotobacter includes, but is not limited to, azospirillum (Azospiralum) and Azotobacter (Azotobacterium) and the like, and phosphate-solubilizing bacteria includes, but is not limited to, bacillus (Bacillus) and Pseudomonas (Pseudomonas) and the like. The nitrogen fixing bacteria can help plants fix nitrogen sources from air, the phosphate dissolving bacteria can convert indissolvable phosphorus in soil into absorbable forms, and the plant growth is promoted, and the dosage of the phosphate dissolving bacteria is 0.2% of the mass of decomposed straw.|[0038] Then mixing the functional material, the compound microbial agent and the decomposed straw to obtain Tian Wuliao, and uniformly spreading the returning material into a target area (a soil layer of 0-20 cm in the target area) of which the soil needs to be improved according to the dosage of 4.5 tons per hectare;|[0039] step three, monitoring and controlling after application |[0040] After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result. Wherein pH is measured every half year, CO 2 emission and N 2 O emission are measured after rainy season (N 2 O high-onset period) and autumn harvest (CO 2 high-onset period), which can be measured by using a portable gas chromatograph.|[0041] Correspondingly, the specific mode of the regulation treatment is as follows:|[0042] when the pH value is less than 5.5, the soil is continuously acidified, and the application amount of alkaline materials is required to be increased for neutralization, so that the consumption of returning materials is increased by 1 ton per hectare, namely, 1 ton is increased on the initial consumption of 4.5 tons per hectare, and then, the consumption of returning materials is 5.5 tons per hectare in the next production season; |[0043] When the CO 2 emission value is more than 500 mg/(m 2 h), the mineralization activity of soil microorganisms is too strong, and organic carbon is decomposed too fast and is unfavorable for carbon fixation, so that the dosage of decomposed straw in returning materials is reduced by 10 percent (based on the initial dosage in the last season) in the next production season, and the dosage of other materials is reduced based on the dosage of the decomposed straw, namely, the dosage of the other materials is reduced in equal proportion as the dosage of new decomposed straw after the reduction, so that the dosage of returning materials is reduced; |[0044] When the emission value of N 2 O is more than 10 mug/(m 2 h), the denitrification of the soil is strong, the nitrogen is lost in a gas form, and the dosage of the compound microbial inoculant in the returning materials is increased by 5% in the next production season, so that the carbon-nitrogen ratio is balanced by enhancing the biological nitrogen fixation effect. The consumption of the rest materials is unchanged. |[0045] Example two|[0046] According to the embodiment shown in fig. 1, the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment is provided, and comprises the following steps:|[0047] Step one, preparing straw and performing differentiation treatment |[0048] Suitable straw materials (rice straw, corn straw, wheat straw and bagasse) are selected, and differential crushing treatment is performed according to straw material characteristics (lignification degree and fiber structure), wherein the rice straw and the bagasse are crushed to 4cm, and the corn straw and the wheat straw are crushed to 3m. Specifically, for rice straw, the rice straw contains lower lignin, the fiber is softer and is easy to decompose, if the fiber is too thin (less than 2 cm), the fiber can cause early decay or loss in the composting process, if the fiber is too thick (more than 5 cm), the decomposition speed is slow, and the composting period is prolonged, so that the embodiment adopts the design of 4cm, not only can ensure enough microorganism adhesion surface area, but also can prevent excessive smashing to cause excessive accumulation, poor air permeability or nutrient loss with water in a humid environment. For bagasse, the bagasse contains higher fibers and less lignin, has higher toughness, can ensure moderate decomposition speed by crushing to the grain size of 4cm, can better utilize the microbial activity generated in the composting process, and keeps enough space for oxidation reaction. For corn straw and wheat straw, the lignin content is higher, the fiber toughness is strong, so that the contact area between the corn straw and microorganisms can be increased by crushing the corn straw and the wheat straw to the grain size of 3cm, the decomposition is promoted, the decomposition speed is slow due to overhigh (more than 5 cm), and the difficulty in retting is increased due to overlong (less than 2 cm). Therefore, the differential crushing can not only improve the decomposition efficiency, but also ensure the stability of the straws and the virtuous circle of the microbial activity in the composting process, and avoid the incomplete decomposition problem caused by different types of the straws.|[0049] And then mixing the mixture with livestock manure (cow manure) according to a mass ratio of 8:2, adding lime in an amount which is 2.5% of the weight of the crushed straw in the mixing process, and adjusting the pH value to be within a range of 6.0-6.5, thereby obtaining the tempering mixture after the mixing is completed. In the mixing process, lime is used for neutralizing organic acid in the pile body, and the pH value is regulated to be in the range of 6.0-6.5, so that the activity of microorganisms in the composting process is facilitated, and the ventilation and decomposition effects of the pile body are ensured.|[0050] Carrying out differential stack retting treatment on the quenched and tempered mixture to obtain decomposed straws, wherein the specific mode of the differential stack retting treatment is as follows:|[0051] For rice straw and bagasse, the stacking height is 1.2 meters, so that internal anaerobic caused by excessive stacking is prevented. The surface layer is covered with dried straw with the thickness of 5cm for moisture preservation and rain prevention. The composting period is 45 days. When the temperature of the center of the pile body is raised to 55 ℃ or above, turning the pile for 1 time in the whole period, namely turning once every 30 days, wherein the turning aims at radiating heat and cooling, supplementing oxygen, preventing the pile from being burned and promoting uniform decomposition; |[0052] For corn straw and wheat straw, the corn straw and wheat straw are piled up by 1.5 meters to reduce water evaporation, covered with a mulching film to preserve soil moisture, and piled up for 60 days in a composting period, water is sprayed 1 time every 15 days, so that the water content of the piled up body is kept within the range of 60% -65%, and the metabolic activity of microorganisms is ensured. |[0053] Monitoring the temperature, color, texture and smell of the piled body in the composting process, and judging that the thoroughly decomposed straw is obtained when the temperature of the piled body is reduced to below 30 ℃, the color of the piled body is changed into dark brown, the piled body is easy to pinch by hands, the piled body has no acid odor and the pH value of the piled body is stable within the range of 6.0-7.0.|[0054] Step two, preparation and application of Tian Wuliao|[0055] The functional materials comprise biochar and desulfurized gypsum, the biochar is specifically prepared by carrying out slow pyrolysis on peanut shells (local agricultural wastes) for 4 hours at 400 ℃, the particle size is 3mm, the biochar has a good porous structure, the physicochemical property of soil is improved, the dosage of the biochar is 80% of the mass of decomposed straw, the desulfurized gypsum contains higher calcium element, the acidity of the soil can be effectively neutralized, the soil structure is improved, meanwhile, the heavy metal lead and cadmium contents are all lower than 100mg/kg, the safety of the desulfurized gypsum is ensured, and the corresponding dosage is 50% of the mass of the decomposed straw.|[0056] For the microbial agent, a commercially available composite microbial agent is selected and contains effective azotobacter and phosphate-dissolving bacteria. Azotobacter includes, but is not limited to, azospirillum (Azospiralum) and Azotobacter (Azotobacterium) and the like, and phosphate-solubilizing bacteria includes, but is not limited to, bacillus (Bacillus) and Pseudomonas (Pseudomonas) and the like. The nitrogen fixing bacteria can help plants fix nitrogen sources from air, the phosphate dissolving bacteria can convert indissolvable phosphorus in soil into absorbable forms, and the plant growth is promoted, and the dosage of the phosphate dissolving bacteria is 0.3% of the mass of decomposed straw.|[0057] Then mixing the functional material, the compound microbial agent and the decomposed straw to obtain Tian Wuliao, and uniformly spreading the returning material into a target area (a soil layer of 0-20 cm in the target area) in which soil needs to be improved according to the dosage of 6 tons per hectare;|[0058] step three, monitoring and controlling after application |[0059] After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result. Wherein pH is measured every half year, CO 2 emission and N 2 O emission are measured after rainy season (N 2 O high-onset period) and autumn harvest (CO 2 high-onset period), which can be measured by using a portable gas chromatograph.|[0060] Correspondingly, the specific mode of the regulation treatment is as follows:|[0061] When the pH value is less than 5.5, the soil is continuously acidified, and the application amount of alkaline materials is required to be increased for neutralization, so that the consumption of returning materials is increased by 1 ton per hectare, namely, 1 ton is increased on the initial consumption of 6 tons per hectare, and then, the consumption of returning materials is 7 tons per hectare in the next production season; |[0062] When the CO 2 emission value is more than 500 mg/(m 2 h), the mineralization activity of soil microorganisms is too strong, and organic carbon is decomposed too fast and is unfavorable for carbon fixation, so that the dosage of decomposed straw in returning materials is reduced by 10 percent (based on the initial dosage in the last season) in the next production season, and the dosage of other materials is reduced based on the dosage of the decomposed straw, namely, the dosage of the other materials is reduced in equal proportion as the dosage of new decomposed straw after the reduction, so that the dosage of returning materials is reduced; |[0063] When the emission value of N 2 O is more than 10 mug/(m 2 h), the denitrification of the soil is strong, the nitrogen is lost in a gas form, and the dosage of the compound microbial inoculant in the returning materials is increased by 5% in the next production season, so that the carbon-nitrogen ratio is balanced by enhancing the biological nitrogen fixation effect. The consumption of the rest materials is unchanged. |[0064] Example III|[0065] According to the embodiment shown in fig. 1, the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment is provided, and comprises the following steps:|[0066] Step one, preparing straw and performing differentiation treatment |[0067] Suitable straw materials (rice straw, corn straw, wheat straw and bagasse) are selected, and differential crushing treatment is performed according to straw material characteristics (lignification degree and fiber structure), wherein the rice straw and the bagasse are crushed to 5cm, and the corn straw and the wheat straw are crushed to 4m. Specifically, for rice straw, the rice straw contains lower lignin, the fiber is softer and is easy to decompose, if the fiber is too thin (less than 2 cm), the fiber can cause early decay or loss in the composting process, if the fiber is too thick (more than 5 cm), the decomposition speed is slow, and the composting period is prolonged, so that the embodiment adopts the design of 5cm, not only can ensure enough microorganism adhesion surface area, but also can prevent excessive smashing to cause excessive accumulation, poor air permeability or nutrient loss with water in a humid environment. For bagasse, the bagasse contains higher fibers and less lignin, has higher toughness, can ensure moderate decomposition speed by crushing to a grain size of 5cm, can better utilize microbial activity generated in the composting process, and keeps enough space for oxidation reaction. For corn straw and wheat straw, the lignin content is higher, the fiber toughness is strong, so that the contact area between the corn straw and microorganisms can be increased by crushing the corn straw and the wheat straw to the grain size of 4cm, the decomposition is promoted, the decomposition speed is slow due to overhigh (more than 5 cm), and the difficulty in retting is increased due to overlong (less than 2 cm). Therefore, the differential crushing can not only improve the decomposition efficiency, but also ensure the stability of the straws and the virtuous circle of the microbial activity in the composting process, and avoid the incomplete decomposition problem caused by different types of the straws.|[0068] And then mixing the mixture with livestock manure (cow manure) according to a mass ratio of 8:2, adding lime in an amount which is 3% of the weight of the crushed straw in the mixing process, and adjusting the pH value to be within a range of 6.0-6.5, thereby obtaining the tempering mixture after the mixing is completed. In the mixing process, lime is used for neutralizing organic acid in the pile body, and the pH value is regulated to be in the range of 6.0-6.5, so that the activity of microorganisms in the composting process is facilitated, and the ventilation and decomposition effects of the pile body are ensured.|[0069] Carrying out differential stack retting treatment on the quenched and tempered mixture to obtain decomposed straws, wherein the specific mode of the differential stack retting treatment is as follows:|[0070] For rice straw and bagasse, the stacking height is 1.2 meters, so that internal anaerobic caused by excessive stacking is prevented. The surface layer is covered with dried straw with the thickness of 5cm for moisture preservation and rain prevention. The composting period is 45 days. When the temperature of the center of the pile body is raised to 55 ℃ or above, turning the pile for 1 time in the whole period, namely turning once every 30 days, wherein the turning aims at radiating heat and cooling, supplementing oxygen, preventing the pile from being burned and promoting uniform decomposition; |[0071] For corn straw and wheat straw, the corn straw and wheat straw are piled up by 1.5 meters to reduce water evaporation, covered with a mulching film to preserve soil moisture, and piled up for 60 days in a composting period, water is sprayed 1 time every 15 days, so that the water content of the piled up body is kept within the range of 60% -65%, and the metabolic activity of microorganisms is ensured. |[0072] Monitoring the temperature, color, texture and smell of the piled body in the composting process, and judging that the thoroughly decomposed straw is obtained when the temperature of the piled body is reduced to below 30 ℃, the color of the piled body is changed into dark brown, the piled body is easy to pinch by hands, the piled body has no acid odor and the pH value of the piled body is stable within the range of 6.0-7.0.|[0073] Step two, preparation and application of Tian Wuliao|[0074] The functional materials comprise biochar and desulfurized gypsum, the biochar is specifically prepared by carrying out slow pyrolysis on peanut shells (local agricultural wastes) for 2 hours at the temperature of 500 ℃, the particle size is 5mm, the biochar has a good porous structure and is favorable for improving the physicochemical property of soil, the dosage of the biochar is 100% of the mass of decomposed straw, the desulfurized gypsum contains higher calcium element, the acidity of the soil can be effectively neutralized, the soil structure is improved, meanwhile, the contents of heavy metals lead and cadmium are lower than 100mg/kg, the safety of the desulfurized gypsum is ensured, and the corresponding dosage is 60% of the mass of the decomposed straw.|[0075] For the microbial agent, a commercially available composite microbial agent is selected and contains effective azotobacter and phosphate-dissolving bacteria. Azotobacter includes, but is not limited to, azospirillum (Azospiralum) and Azotobacter (Azotobacterium) and the like, and phosphate-solubilizing bacteria includes, but is not limited to, bacillus (Bacillus) and Pseudomonas (Pseudomonas) and the like. The nitrogen fixing bacteria can help plants fix nitrogen sources from air, the phosphate dissolving bacteria can convert indissolvable phosphorus in soil into absorbable forms, and the plant growth is promoted, and the dosage of the phosphate dissolving bacteria is 0.4% of the mass of decomposed straw.|[0076] Then mixing the functional material, the compound microbial agent and the decomposed straw to obtain Tian Wuliao, and uniformly spreading the returning material into a target area (a soil layer of 0-20 cm in the target area) in which soil needs to be improved according to the use amount of 8 tons per hectare;|[0077] step three, monitoring and controlling after application |[0078] After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result. Wherein pH is measured every half year, CO 2 emission and N 2 O emission are measured after rainy season (N 2 O high-onset period) and autumn harvest (CO 2 high-onset period), which can be measured by using a portable gas chromatograph.|[0079] Correspondingly, the specific mode of the regulation treatment is as follows:|[0080] When the pH value is less than 5.5, the soil is continuously acidified, and the application amount of alkaline materials is required to be increased for neutralization, so that the consumption of returning materials is increased by 1 ton per hectare, namely, 1 ton is increased on the initial consumption of 8 tons per hectare, and then, the consumption of returning materials is 9 tons per hectare in the next production season; |[0081] When the CO 2 emission value is more than 500 mg/(m 2 h), the mineralization activity of soil microorganisms is too strong, and organic carbon is decomposed too fast and is unfavorable for carbon fixation, so that the dosage of decomposed straw in returning materials is reduced by 10 percent (based on the initial dosage in the last season) in the next production season, and the dosage of other materials is reduced based on the dosage of the decomposed straw, namely, the dosage of the other materials is reduced in equal proportion as the dosage of new decomposed straw after the reduction, so that the dosage of returning materials is reduced; |[0082] When the emission value of N 2 O is more than 10 mug/(m 2 h), the denitrification of the soil is strong, the nitrogen is lost in a gas form, and the dosage of the compound microbial inoculant in the returning materials is increased by 5% in the next production season, so that the carbon-nitrogen ratio is balanced by enhancing the biological nitrogen fixation effect. The consumption of the rest materials is unchanged. |[0083] In combination with the first, second and third examples, untreated soil was used as a control group, and the production cycle was measured for one year, and the results were compared in performance as shown in the following table:|[0084] |[0085] |[0086] As shown in the above table, when the amount of Tian Wuliao is larger, the amount of inputted organic carbon is larger, so that the organic carbon increase of the soil is maximum, and the carbon fixing effect is most remarkable. Meanwhile, lime, biochar (alkaline) and alkaline substances generated by decomposing decomposed straw in the returning materials jointly neutralize the acidity of the soil, and the invention converts straw waste into valuable resources for improving the acid soil, thereby realizing multiple aims of treating waste with waste, fixing carbon, reducing emission, increasing yield and improving efficiency. |[0087] The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the scope of the invention as defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof. (CN121286156)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the field of soil improvement technology and low-carbon production, in particular to a method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment.|BACKGROUND ART|[0002] With the increasing global climate change problem, farmland greenhouse gas emissions (especially methane and nitrous oxide) are attracting more and more attention. In agricultural production activities, especially soil management and crop production, are one of the important sources of greenhouse gas emissions. However, most cultivated lands in China have the problem of acidification, a large amount of farmland soil belongs to acid soil (pH value is less than 5.5), and the farmland soil usually lacks alkaline mineral elements such as calcium, magnesium and the like, which are critical to the growth of crops, and meanwhile, many beneficial soil microorganisms (such as azotobacter, phosphate-dissolving bacteria and the like) have lower activity in the acid soil, so that the soil fertility is insufficient, the emission of greenhouse gases is high, and the growth of crops and the green production of agriculture are limited.|[0003] Therefore, the improvement of acid soil and carbon sequestration and emission reduction are always one of important research directions in the agricultural field. In the prior art, the improvement of acid soil mainly depends on the neutralization by using alkaline substances such as lime, serpentine and the like, and the improvement of soil structure by returning organic substances (such as straw, agricultural and forestry waste and the like) to fields, thereby improving soil fertility and carbon reserves. For the traditional improvement mode of returning the straws to the field, the decomposition period is longer, the influence of the climatic conditions is larger, the incomplete decomposition of the straws, the loss of nutrients and the increase of greenhouse gas emission are easily caused, and the long-term health of soil and the agricultural green production level are influenced, so the invention provides a method for improving the carbon sequestration and emission reduction capability of acid soil based on straw treatment to solve the problems in the prior art.|DISCLOSURE|Disclosure of Invention|[0004] In view of the above problems, the present invention aims to provide a method for improving the carbon sequestration and emission reduction capacity of acidic soil based on straw treatment, which improves the accumulation of organic carbon in the soil, not only improves the soil fertility, but also reduces the carbon dioxide concentration in the atmosphere through the carbon fixation effect and relieves the greenhouse gas effect.|[0005] The invention aims at realizing the aim by adopting the following technical scheme that the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment comprises the following steps:|[0006] Step one, preparing straw and performing differentiation treatment |[0007] Preparing straw materials, carrying out differential crushing treatment according to the characteristics of the straw materials to obtain crushed straw, mixing the crushed straw with livestock manure according to a mass ratio of 8:2, adding lime in an amount of 2-3% of the weight of the crushed straw in the mixing process, adjusting the pH value of the mixed material to 6.0-6.5 to obtain a quenched and tempered mixed material, and carrying out differential composting treatment on the quenched and tempered mixed material to obtain decomposed straw;|[0008] Step two, preparation and application of Tian Wuliao |[0009] Preparing a compounded functional material and a compound microbial agent, wherein the functional material comprises biochar and desulfurized gypsum, the compound microbial agent is a compound microbial agent containing azotobacter and phosphate-dissolving bacteria, then the functional material and the compound microbial agent are mixed with decomposed straws to obtain Tian Wuliao, and then the returning material is uniformly spread in a target area in which soil needs to be improved according to the use amount of 4.5-8 tons per hectare;|[0010] step three, monitoring and controlling after application |[0011] After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result.|[0012] The method is further improved in that in the first step, the straw material is one of rice straw, corn straw, wheat straw and bagasse, wherein the rice straw and the bagasse are crushed to 3-5 cm, and the corn straw and the wheat straw are crushed to 2-4 cm.|[0013] The method is further improved in that in the first step, the judging standard of the decomposed straw is that the decomposition is judged to be completed when the temperature of the pile body is reduced to below 30 ℃, the color of the pile body is changed to dark brown, the pile body is fragile by hand pinching, the pile body has no acid odor, and the pH value of the pile body is stabilized at 6.0-7.0.|[0014] The method is further improved in that in the second step, the biochar is prepared by carrying out slow pyrolysis on peanut shells for 2-4 hours at the temperature of 300-500 ℃, the particle size is 2-5 mm, and the dosage of the biochar is 60-100% of the mass of the decomposed straw.|[0015] The method is further improved in that in the second step, the content of heavy metals lead and cadmium in the desulfurized gypsum is lower than 100mg/kg, and the dosage of the heavy metals lead and cadmium in the desulfurized gypsum is 40-60% of the mass of the decomposed straw.|[0016] The method is further improved in that in the second step, the dosage of the composite microbial agent is 0.2-0.4% of the mass of the decomposed straw.|[0017] The further improvement is that in the third step, the pH value is measured every half year, and the CO 2 emission value and the N 2 O emission value are measured after rainy season and autumn harvest.|[0018] The method is further improved in that in the third step, the specific mode of regulation and control treatment is as follows:|[0019] when the pH value is less than 5.5, the consumption of returning materials is increased by 1-2 tons per hectare; |[0020] When the CO 2 emission value is more than 500 mg/(m 2.h), the dosage of decomposed straw in the returning materials is reduced by 10 percent; |[0021] When the emission value of N 2 O is more than 10 mug/(m 2 h), the dosage of the composite microbial agent in the returning materials is increased by 5%. |[0022] The method has the beneficial effects that differential crushing treatment and differential stack retting treatment are carried out according to the characteristics of straw materials, so that the straw treatment link is optimized, the decomposition period is shortened, the quality uniformity of returning materials is ensured, the problems of incomplete decomposition or nutrient loss caused by material difference are solved, the biochar is prepared by utilizing agricultural waste peanut shells in a low-cost material compounding manner, industrial byproduct desulfurized gypsum is used for replacing commodity gypsum, the cost of preparing materials is reduced, and the accumulation amount and stability of organic carbon in soil are improved through the synergistic cooperation of the decomposed straw and the biochar, so that the effect of improving the carbon fixation and emission reduction capability of acid soil is achieved.|DRAWINGS DESCRIPTION|[0023] FIG. 1 is a schematic flow chart of the steps of the present invention.|INVENTION MODE|Detailed Description|[0024] The present invention will be further described in detail with reference to the following examples, which are only for the purpose of illustrating the invention and are not to be construed as limiting the scope of the invention.|[0025] In the examples below, the sources of materials are all commercially available.|[0026] Example 1|[0027] According to the embodiment shown in fig. 1, the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment is provided, and comprises the following steps:|[0028] Step one, preparing straw and performing differentiation treatment |[0029] Suitable straw materials (rice straw, corn straw, wheat straw and bagasse) are selected, and differential crushing treatment is performed according to straw material characteristics (lignification degree and fiber structure), wherein the rice straw and the bagasse are crushed to 3cm, and the corn straw and the wheat straw are crushed to 2m. Specifically, for rice straw, the rice straw contains lower lignin, the fiber is softer and is easy to decompose, if the fiber is too thin (less than 2 cm), the fiber can cause early decay or loss in the composting process, if the fiber is too thick (more than 5 cm), the decomposition speed is slow, and the composting period is prolonged, so that the embodiment adopts a 3cm design, not only can ensure enough microorganism adhesion surface area, but also can prevent excessive smashing to cause excessive accumulation, poor air permeability or nutrient loss with water in a humid environment. For bagasse, the bagasse contains higher fibers and less lignin, has higher toughness, can ensure moderate decomposition speed by crushing to 3cm particle size, can better utilize microbial activity generated in the composting process, and keeps enough space for oxidation reaction. For corn straw and wheat straw, the lignin content is higher, the fiber toughness is strong, so that the contact area between the corn straw and microorganisms can be increased by crushing the corn straw and the wheat straw to 2cm, the decomposition is promoted, the decomposition speed is slow due to overhigh (more than 5 cm), and the difficulty in retting can be increased due to overlong (less than 2 cm). Therefore, the differential crushing can not only improve the decomposition efficiency, but also ensure the stability of the straws and the virtuous circle of the microbial activity in the composting process, and avoid the incomplete decomposition problem caused by different types of the straws.|[0030] And then mixing the mixture with livestock manure (cow manure) according to a mass ratio of 8:2, adding lime in an amount which is 2% of the weight of the crushed straw in the mixing process, and adjusting the pH value to be within a range of 6.0-6.5, thereby obtaining the tempering mixture after the mixing is completed. In the mixing process, lime is used for neutralizing organic acid in the pile body, and the pH value is regulated to be in the range of 6.0-6.5, so that the activity of microorganisms in the composting process is facilitated, and the ventilation and decomposition effects of the pile body are ensured.|[0031] Carrying out differential stack retting treatment on the quenched and tempered mixture to obtain decomposed straws, wherein the specific mode of the differential stack retting treatment is as follows:|[0032] For rice straw and bagasse, the stacking height is 1.0 meter, so that internal anaerobic caused by excessive stacking is prevented. The surface layer is covered with dried straw with the thickness of 5cm for moisture preservation and rain prevention. The composting period is 45 days. When the temperature of the center of the pile body is raised to 55 ℃ or above, turning the pile for 1 time in the whole period, namely turning once every 30 days, wherein the turning aims at radiating heat and cooling, supplementing oxygen, preventing the pile from being burned and promoting uniform decomposition; |[0033] For corn straw and wheat straw, the corn straw and wheat straw are piled up by 1.5 meters to reduce water evaporation, covered with a mulching film to preserve soil moisture, and piled up for 60 days in a composting period, water is sprayed 1 time every 15 days, so that the water content of the piled up body is kept within the range of 60% -65%, and the metabolic activity of microorganisms is ensured. |[0034] Monitoring the temperature, color, texture and smell of the piled body in the composting process, and judging that the thoroughly decomposed straw is obtained when the temperature of the piled body is reduced to below 30 ℃, the color of the piled body is changed into dark brown, the piled body is easy to pinch by hands, the piled body has no acid odor and the pH value of the piled body is stable within the range of 6.0-7.0.|[0035] Step two, preparation and application of Tian Wuliao|[0036] The functional materials comprise biochar and desulfurized gypsum, the biochar is specifically prepared by carrying out low-speed pyrolysis on peanut shells (local agricultural wastes) for 4 hours at the temperature of 300 ℃, the particle size is 2mm, the biochar has a good porous structure and is favorable for improving the physicochemical property of soil, the dosage of the biochar is 60% of the mass of decomposed straw, the desulfurized gypsum contains higher calcium element, the acidity of the soil can be effectively neutralized, the soil structure is improved, meanwhile, the heavy metal lead and cadmium contents of the desulfurized gypsum are all lower than 100mg/kg, the safety of the desulfurized gypsum is ensured, and the corresponding dosage is 40% of the mass of the decomposed straw.|[0037] For the microbial agent, a commercially available composite microbial agent is selected and contains effective azotobacter and phosphate-dissolving bacteria. Azotobacter includes, but is not limited to, azospirillum (Azospiralum) and Azotobacter (Azotobacterium) and the like, and phosphate-solubilizing bacteria includes, but is not limited to, bacillus (Bacillus) and Pseudomonas (Pseudomonas) and the like. The nitrogen fixing bacteria can help plants fix nitrogen sources from air, the phosphate dissolving bacteria can convert indissolvable phosphorus in soil into absorbable forms, and the plant growth is promoted, and the dosage of the phosphate dissolving bacteria is 0.2% of the mass of decomposed straw.|[0038] Then mixing the functional material, the compound microbial agent and the decomposed straw to obtain Tian Wuliao, and uniformly spreading the returning material into a target area (a soil layer of 0-20 cm in the target area) of which the soil needs to be improved according to the dosage of 4.5 tons per hectare;|[0039] step three, monitoring and controlling after application |[0040] After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result. Wherein pH is measured every half year, CO 2 emission and N 2 O emission are measured after rainy season (N 2 O high-onset period) and autumn harvest (CO 2 high-onset period), which can be measured by using a portable gas chromatograph.|[0041] Correspondingly, the specific mode of the regulation treatment is as follows:|[0042] when the pH value is less than 5.5, the soil is continuously acidified, and the application amount of alkaline materials is required to be increased for neutralization, so that the consumption of returning materials is increased by 1 ton per hectare, namely, 1 ton is increased on the initial consumption of 4.5 tons per hectare, and then, the consumption of returning materials is 5.5 tons per hectare in the next production season; |[0043] When the CO 2 emission value is more than 500 mg/(m 2 h), the mineralization activity of soil microorganisms is too strong, and organic carbon is decomposed too fast and is unfavorable for carbon fixation, so that the dosage of decomposed straw in returning materials is reduced by 10 percent (based on the initial dosage in the last season) in the next production season, and the dosage of other materials is reduced based on the dosage of the decomposed straw, namely, the dosage of the other materials is reduced in equal proportion as the dosage of new decomposed straw after the reduction, so that the dosage of returning materials is reduced; |[0044] When the emission value of N 2 O is more than 10 mug/(m 2 h), the denitrification of the soil is strong, the nitrogen is lost in a gas form, and the dosage of the compound microbial inoculant in the returning materials is increased by 5% in the next production season, so that the carbon-nitrogen ratio is balanced by enhancing the biological nitrogen fixation effect. The consumption of the rest materials is unchanged. |[0045] Example two|[0046] According to the embodiment shown in fig. 1, the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment is provided, and comprises the following steps:|[0047] Step one, preparing straw and performing differentiation treatment |[0048] Suitable straw materials (rice straw, corn straw, wheat straw and bagasse) are selected, and differential crushing treatment is performed according to straw material characteristics (lignification degree and fiber structure), wherein the rice straw and the bagasse are crushed to 4cm, and the corn straw and the wheat straw are crushed to 3m. Specifically, for rice straw, the rice straw contains lower lignin, the fiber is softer and is easy to decompose, if the fiber is too thin (less than 2 cm), the fiber can cause early decay or loss in the composting process, if the fiber is too thick (more than 5 cm), the decomposition speed is slow, and the composting period is prolonged, so that the embodiment adopts the design of 4cm, not only can ensure enough microorganism adhesion surface area, but also can prevent excessive smashing to cause excessive accumulation, poor air permeability or nutrient loss with water in a humid environment. For bagasse, the bagasse contains higher fibers and less lignin, has higher toughness, can ensure moderate decomposition speed by crushing to the grain size of 4cm, can better utilize the microbial activity generated in the composting process, and keeps enough space for oxidation reaction. For corn straw and wheat straw, the lignin content is higher, the fiber toughness is strong, so that the contact area between the corn straw and microorganisms can be increased by crushing the corn straw and the wheat straw to the grain size of 3cm, the decomposition is promoted, the decomposition speed is slow due to overhigh (more than 5 cm), and the difficulty in retting is increased due to overlong (less than 2 cm). Therefore, the differential crushing can not only improve the decomposition efficiency, but also ensure the stability of the straws and the virtuous circle of the microbial activity in the composting process, and avoid the incomplete decomposition problem caused by different types of the straws.|[0049] And then mixing the mixture with livestock manure (cow manure) according to a mass ratio of 8:2, adding lime in an amount which is 2.5% of the weight of the crushed straw in the mixing process, and adjusting the pH value to be within a range of 6.0-6.5, thereby obtaining the tempering mixture after the mixing is completed. In the mixing process, lime is used for neutralizing organic acid in the pile body, and the pH value is regulated to be in the range of 6.0-6.5, so that the activity of microorganisms in the composting process is facilitated, and the ventilation and decomposition effects of the pile body are ensured.|[0050] Carrying out differential stack retting treatment on the quenched and tempered mixture to obtain decomposed straws, wherein the specific mode of the differential stack retting treatment is as follows:|[0051] For rice straw and bagasse, the stacking height is 1.2 meters, so that internal anaerobic caused by excessive stacking is prevented. The surface layer is covered with dried straw with the thickness of 5cm for moisture preservation and rain prevention. The composting period is 45 days. When the temperature of the center of the pile body is raised to 55 ℃ or above, turning the pile for 1 time in the whole period, namely turning once every 30 days, wherein the turning aims at radiating heat and cooling, supplementing oxygen, preventing the pile from being burned and promoting uniform decomposition; |[0052] For corn straw and wheat straw, the corn straw and wheat straw are piled up by 1.5 meters to reduce water evaporation, covered with a mulching film to preserve soil moisture, and piled up for 60 days in a composting period, water is sprayed 1 time every 15 days, so that the water content of the piled up body is kept within the range of 60% -65%, and the metabolic activity of microorganisms is ensured. |[0053] Monitoring the temperature, color, texture and smell of the piled body in the composting process, and judging that the thoroughly decomposed straw is obtained when the temperature of the piled body is reduced to below 30 ℃, the color of the piled body is changed into dark brown, the piled body is easy to pinch by hands, the piled body has no acid odor and the pH value of the piled body is stable within the range of 6.0-7.0.|[0054] Step two, preparation and application of Tian Wuliao|[0055] The functional materials comprise biochar and desulfurized gypsum, the biochar is specifically prepared by carrying out slow pyrolysis on peanut shells (local agricultural wastes) for 4 hours at 400 ℃, the particle size is 3mm, the biochar has a good porous structure, the physicochemical property of soil is improved, the dosage of the biochar is 80% of the mass of decomposed straw, the desulfurized gypsum contains higher calcium element, the acidity of the soil can be effectively neutralized, the soil structure is improved, meanwhile, the heavy metal lead and cadmium contents are all lower than 100mg/kg, the safety of the desulfurized gypsum is ensured, and the corresponding dosage is 50% of the mass of the decomposed straw.|[0056] For the microbial agent, a commercially available composite microbial agent is selected and contains effective azotobacter and phosphate-dissolving bacteria. Azotobacter includes, but is not limited to, azospirillum (Azospiralum) and Azotobacter (Azotobacterium) and the like, and phosphate-solubilizing bacteria includes, but is not limited to, bacillus (Bacillus) and Pseudomonas (Pseudomonas) and the like. The nitrogen fixing bacteria can help plants fix nitrogen sources from air, the phosphate dissolving bacteria can convert indissolvable phosphorus in soil into absorbable forms, and the plant growth is promoted, and the dosage of the phosphate dissolving bacteria is 0.3% of the mass of decomposed straw.|[0057] Then mixing the functional material, the compound microbial agent and the decomposed straw to obtain Tian Wuliao, and uniformly spreading the returning material into a target area (a soil layer of 0-20 cm in the target area) in which soil needs to be improved according to the dosage of 6 tons per hectare;|[0058] step three, monitoring and controlling after application |[0059] After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result. Wherein pH is measured every half year, CO 2 emission and N 2 O emission are measured after rainy season (N 2 O high-onset period) and autumn harvest (CO 2 high-onset period), which can be measured by using a portable gas chromatograph.|[0060] Correspondingly, the specific mode of the regulation treatment is as follows:|[0061] When the pH value is less than 5.5, the soil is continuously acidified, and the application amount of alkaline materials is required to be increased for neutralization, so that the consumption of returning materials is increased by 1 ton per hectare, namely, 1 ton is increased on the initial consumption of 6 tons per hectare, and then, the consumption of returning materials is 7 tons per hectare in the next production season; |[0062] When the CO 2 emission value is more than 500 mg/(m 2 h), the mineralization activity of soil microorganisms is too strong, and organic carbon is decomposed too fast and is unfavorable for carbon fixation, so that the dosage of decomposed straw in returning materials is reduced by 10 percent (based on the initial dosage in the last season) in the next production season, and the dosage of other materials is reduced based on the dosage of the decomposed straw, namely, the dosage of the other materials is reduced in equal proportion as the dosage of new decomposed straw after the reduction, so that the dosage of returning materials is reduced; |[0063] When the emission value of N 2 O is more than 10 mug/(m 2 h), the denitrification of the soil is strong, the nitrogen is lost in a gas form, and the dosage of the compound microbial inoculant in the returning materials is increased by 5% in the next production season, so that the carbon-nitrogen ratio is balanced by enhancing the biological nitrogen fixation effect. The consumption of the rest materials is unchanged. |[0064] Example III|[0065] According to the embodiment shown in fig. 1, the method for improving the carbon sequestration and emission reduction capacity of the acid soil based on straw treatment is provided, and comprises the following steps:|[0066] Step one, preparing straw and performing differentiation treatment |[0067] Suitable straw materials (rice straw, corn straw, wheat straw and bagasse) are selected, and differential crushing treatment is performed according to straw material characteristics (lignification degree and fiber structure), wherein the rice straw and the bagasse are crushed to 5cm, and the corn straw and the wheat straw are crushed to 4m. Specifically, for rice straw, the rice straw contains lower lignin, the fiber is softer and is easy to decompose, if the fiber is too thin (less than 2 cm), the fiber can cause early decay or loss in the composting process, if the fiber is too thick (more than 5 cm), the decomposition speed is slow, and the composting period is prolonged, so that the embodiment adopts the design of 5cm, not only can ensure enough microorganism adhesion surface area, but also can prevent excessive smashing to cause excessive accumulation, poor air permeability or nutrient loss with water in a humid environment. For bagasse, the bagasse contains higher fibers and less lignin, has higher toughness, can ensure moderate decomposition speed by crushing to a grain size of 5cm, can better utilize microbial activity generated in the composting process, and keeps enough space for oxidation reaction. For corn straw and wheat straw, the lignin content is higher, the fiber toughness is strong, so that the contact area between the corn straw and microorganisms can be increased by crushing the corn straw and the wheat straw to the grain size of 4cm, the decomposition is promoted, the decomposition speed is slow due to overhigh (more than 5 cm), and the difficulty in retting is increased due to overlong (less than 2 cm). Therefore, the differential crushing can not only improve the decomposition efficiency, but also ensure the stability of the straws and the virtuous circle of the microbial activity in the composting process, and avoid the incomplete decomposition problem caused by different types of the straws.|[0068] And then mixing the mixture with livestock manure (cow manure) according to a mass ratio of 8:2, adding lime in an amount which is 3% of the weight of the crushed straw in the mixing process, and adjusting the pH value to be within a range of 6.0-6.5, thereby obtaining the tempering mixture after the mixing is completed. In the mixing process, lime is used for neutralizing organic acid in the pile body, and the pH value is regulated to be in the range of 6.0-6.5, so that the activity of microorganisms in the composting process is facilitated, and the ventilation and decomposition effects of the pile body are ensured.|[0069] Carrying out differential stack retting treatment on the quenched and tempered mixture to obtain decomposed straws, wherein the specific mode of the differential stack retting treatment is as follows:|[0070] For rice straw and bagasse, the stacking height is 1.2 meters, so that internal anaerobic caused by excessive stacking is prevented. The surface layer is covered with dried straw with the thickness of 5cm for moisture preservation and rain prevention. The composting period is 45 days. When the temperature of the center of the pile body is raised to 55 ℃ or above, turning the pile for 1 time in the whole period, namely turning once every 30 days, wherein the turning aims at radiating heat and cooling, supplementing oxygen, preventing the pile from being burned and promoting uniform decomposition; |[0071] For corn straw and wheat straw, the corn straw and wheat straw are piled up by 1.5 meters to reduce water evaporation, covered with a mulching film to preserve soil moisture, and piled up for 60 days in a composting period, water is sprayed 1 time every 15 days, so that the water content of the piled up body is kept within the range of 60% -65%, and the metabolic activity of microorganisms is ensured. |[0072] Monitoring the temperature, color, texture and smell of the piled body in the composting process, and judging that the thoroughly decomposed straw is obtained when the temperature of the piled body is reduced to below 30 ℃, the color of the piled body is changed into dark brown, the piled body is easy to pinch by hands, the piled body has no acid odor and the pH value of the piled body is stable within the range of 6.0-7.0.|[0073] Step two, preparation and application of Tian Wuliao|[0074] The functional materials comprise biochar and desulfurized gypsum, the biochar is specifically prepared by carrying out slow pyrolysis on peanut shells (local agricultural wastes) for 2 hours at the temperature of 500 ℃, the particle size is 5mm, the biochar has a good porous structure and is favorable for improving the physicochemical property of soil, the dosage of the biochar is 100% of the mass of decomposed straw, the desulfurized gypsum contains higher calcium element, the acidity of the soil can be effectively neutralized, the soil structure is improved, meanwhile, the contents of heavy metals lead and cadmium are lower than 100mg/kg, the safety of the desulfurized gypsum is ensured, and the corresponding dosage is 60% of the mass of the decomposed straw.|[0075] For the microbial agent, a commercially available composite microbial agent is selected and contains effective azotobacter and phosphate-dissolving bacteria. Azotobacter includes, but is not limited to, azospirillum (Azospiralum) and Azotobacter (Azotobacterium) and the like, and phosphate-solubilizing bacteria includes, but is not limited to, bacillus (Bacillus) and Pseudomonas (Pseudomonas) and the like. The nitrogen fixing bacteria can help plants fix nitrogen sources from air, the phosphate dissolving bacteria can convert indissolvable phosphorus in soil into absorbable forms, and the plant growth is promoted, and the dosage of the phosphate dissolving bacteria is 0.4% of the mass of decomposed straw.|[0076] Then mixing the functional material, the compound microbial agent and the decomposed straw to obtain Tian Wuliao, and uniformly spreading the returning material into a target area (a soil layer of 0-20 cm in the target area) in which soil needs to be improved according to the use amount of 8 tons per hectare;|[0077] step three, monitoring and controlling after application |[0078] After application, the pH value, the CO 2 emission value and the N 2 O emission value of the soil layer of the target area are detected regularly, and the regulation and control treatment is carried out according to the detection result. Wherein pH is measured every half year, CO 2 emission and N 2 O emission are measured after rainy season (N 2 O high-onset period) and autumn harvest (CO 2 high-onset period), which can be measured by using a portable gas chromatograph.|[0079] Correspondingly, the specific mode of the regulation treatment is as follows:|[0080] When the pH value is less than 5.5, the soil is continuously acidified, and the application amount of alkaline materials is required to be increased for neutralization, so that the consumption of returning materials is increased by 1 ton per hectare, namely, 1 ton is increased on the initial consumption of 8 tons per hectare, and then, the consumption of returning materials is 9 tons per hectare in the next production season; |[0081] When the CO 2 emission value is more than 500 mg/(m 2 h), the mineralization activity of soil microorganisms is too strong, and organic carbon is decomposed too fast and is unfavorable for carbon fixation, so that the dosage of decomposed straw in returning materials is reduced by 10 percent (based on the initial dosage in the last season) in the next production season, and the dosage of other materials is reduced based on the dosage of the decomposed straw, namely, the dosage of the other materials is reduced in equal proportion as the dosage of new decomposed straw after the reduction, so that the dosage of returning materials is reduced; |[0082] When the emission value of N 2 O is more than 10 mug/(m 2 h), the denitrification of the soil is strong, the nitrogen is lost in a gas form, and the dosage of the compound microbial inoculant in the returning materials is increased by 5% in the next production season, so that the carbon-nitrogen ratio is balanced by enhancing the biological nitrogen fixation effect. The consumption of the rest materials is unchanged. |[0083] In combination with the first, second and third examples, untreated soil was used as a control group, and the production cycle was measured for one year, and the results were compared in performance as shown in the following table:|[0084] |[0085] |[0086] As shown in the above table, when the amount of Tian Wuliao is larger, the amount of inputted organic carbon is larger, so that the organic carbon increase of the soil is maximum, and the carbon fixing effect is most remarkable. Meanwhile, lime, biochar (alkaline) and alkaline substances generated by decomposing decomposed straw in the returning materials jointly neutralize the acidity of the soil, and the invention converts straw waste into valuable resources for improving the acid soil, thereby realizing multiple aims of treating waste with waste, fixing carbon, reducing emission, increasing yield and improving efficiency. |[0087] The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the scope of the invention as defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof. Family Number|(117384248)|117384248|Abstract|(CN121286156 A)|The invention provides a method for improving the carbon sequestration and emission reduction capacity of acid soil based on straw treatment , and relates to the field of soil improvement technologies and low - carbon production , and the method comprises the three steps of straw preparation and differential treatment , field returning material preparation and application , and monitoring and regulation after application . According to the invention , differential crushing treatment and differential stack retting treatment are carried out according to the characteristics of straw materials , so that the straw treatment link is optimized , the decomposition period is shortened , the quality uniformity of returning materials is ensured , the problem of incomplete decomposition or nutrient loss caused by material difference is solved , and a low - cost material compounding mode is adopted , so that the quality of the returning materials is improved . The agricultural waste peanut shells are used for preparing the biochar , then the industrial byproduct desulfurized gypsum is used for replacing commercial gypsum , the material preparation cost is reduced , then through cooperation of the decomposed straw and the biochar , the accumulation amount and stability of soil organic carbon are improved , and the effect of improving the carbon sequestration and emission reduction capacity of the acid soil is achieved . |IPC codes|(CN121286156 A)|A01B - 079/00 |A01B - 079/02 |Title|(CN121286156 A)|Method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment | Basic materials chemistry|Other special machines A01B-079/00|A01B-079/02|C05D-003/00|C05D-003/02|C05D-009/00|C05F-003/00|C05F-005/00/2|C05F-011/00|C05F-017/00|C05G-003/00|C05G-003/80|C09K-017/14|C09K-017/40|C09K-2101/00|C09K-2109/00|Y02W-030/43 A01B-079/00|A01B-079/02|C05D-003/00|C05D-003/02|C05D-009/00|C05F-003/00|C05F-005/00/2|C05F-011/00|C05F-017/00|C05G-003/00|C05G-003/80|C09K-017/14|C09K-017/40|C09K-2101/00|C09K-2109/00|Y02W-030/43 A01B-079/00|A01B-079/02|C05F-017/20|C05G-003/00|C05G-003/80|C09K-017/40|C09K-101/00|C09K-109/00 A01B-079/00|A01B-079/02|C05F-017/20|C05G-003/00|C05G-003/80|C09K-017/40|C09K-101/00|C09K-109/00 PENDING (CN121286156)|PENDING ALIVE (CN121286156)|ALIVE (CN121286156)|LEGAL DETAILS FOR CN121286156|Actual or expected expiration date=2045-09-28|Legal state=ALIVE|Status=PENDING|Event publication date=2025-09-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511396598|Application date=2025-09-28|Standardized application number=2025CN-1396598|Event publication date=2026-01-09|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121286156|Publication stage code=A|Publication date=2026-01-09|Standardized publication number=CN121286156|Event publication date=2026-01-09|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2026-01-27|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121286156)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKdIF1soYOheAlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080430761&ekey=2216&xpn=CN121286156&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=KUft6pJBhnscrdjavGVzKJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121286156)|CN (CN121286156)|NAME=GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES, INSTITUTE OF AGRICULTURAL RESOURCES AND ENVIRONMENT , COUNTRY=CN (CN121286156)|NAME=SUN JIAN;BEIJING SHENGGUANGXINHE IP FIRM , REG=16117 (CN121286156)|CN (CN121286156)|NAME=HUANG QIAOYI, COUNTRY=CN |NAME=TANG SHUANHU|NAME=WU TENGFEI|NAME=HUANG JIANFENG|NAME=HUANG XU|NAME=ZHANG MU|NAME=YI QIONG|NAME=PANG YUWAN|NAME=DING WUHAN|NAME=CENG KE|NAME=LI PING|NAME=FU HONGTING|NAME=WU YONGPEI|NAME=LUO HAIBIN 0 1 Titre: (CN121286156)|Method for improving carbon sequestration and emission reduction capacity of acid soil based on straw treatment Résumé: (CN121286156)|The invention provides a method for improving the carbon sequestration and emission reduction capacity of acid soil based on straw treatment, and relates to the field of soil improvement technologies and low-carbon production, and the method comprises the three steps of straw preparation and differential treatment, field returning material preparation and application, and monitoring and regulation after application. According to the invention, differential crushing treatment and differential stack retting treatment are carried out according to the characteristics of straw materials, so that the straw treatment link is optimized, the decomposition period is shortened, the quality uniformity of returning materials is ensured, the problem of incomplete decomposition or nutrient loss caused by material difference is solved, and a low-cost material compounding mode is adopted, so that the quality of the returning materials is improved. The agricultural waste peanut shells are used for preparing the biochar, then the industrial byproduct desulfurized gypsum is used for replacing commercial gypsum, the material preparation cost is reduced, then through cooperation of the decomposed straw and the biochar, the accumulation amount and stability of soil organic carbon are improved, and the effect of improving the carbon sequestration and emission reduction capacity of the acid soil is achieved. 31 Abstract gpt-4o-mini no The article focuses on improving carbon sequestration in acid soil through straw treatment and biochar, without addressing mineral weathering or CO₂ capture through mineral carbonation.
31 CN202211191239 CN202211191239 CN115380657 102741067 CN115380657 A 2022-11-25 [CN115380657] 2022-09-28 2022-09-28 2022-11-25 (CN115380657)|2024-09-17 (CN115380657)|Carbon sequestration and emission reduction method based on cooperative returning of vicia sativa and highland barley straw to field (CN115380657)|The invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative returning, and belongs to the technical field of soil improvement. The invention provides a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straw, which comprises the following steps: (1) crushing common vetch and highland barley straw, and mixing with urea and water to obtain a to-be-mixed fertilizer; (2) surface soil is stripped, and core soil is dug out; (3) mixing surface soil with a to-be-mixed fertilizer, filling the mixture into the position where the core soil is dug out, then covering the core soil, and planting crops on the core soil; and (4) repeating the steps (1)-(3) for 1-2 times. According to the method, the common vetch straw and the highland barley straw are cooperatively returned to the field, the soil structure is improved in the mode that surface soil and core soil are alternately fertilized at intervals, a carbon source is supplemented, the carbon sequestration capacity of the soil is improved, and carbon emission is reduced. QINGHAI ACADEMY OF AGRICULTURAL & FORESTRY (CN115380657)|QINGHAI ACADEMY OF AGRICULTURAL & FORESTRY ([CN]) HAN MEI|LI ZHENGPENG (CN115380657)|HAN MEI|LI ZHENGPENG (CN115380657)|DONG DAYUAN;RZBC PATENT AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 11732 (CN115380657)|Therefore, it is necessary to improve and scientifically and reasonably utilize the soil and improve the carbon sequestration capacity of the soil.|Research shows that the change of land utilization modes from grassland and forest land to farmland can cause the loss of organic carbon in soil.| (CN115380657)|1. A carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straw to field is characterized by comprising the following steps:(1) Crushing common vetch and highland barley straws, mixing the crushed common vetch and highland barley straws with urea and water to obtain a fertilizer to be mixed;(2) Stripping surface soil and digging core soil;(3) Mixing surface soil and the fertilizer to be mixed, filling the mixture into the position where core soil is dug out, then covering the core soil, and planting crops on the core soil;(4) Repeating the steps (1) to (3) for 1 to 2 times.| (CN115380657)|The invention aims to provide a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straws to field, and the purposes of soil improvement and carbon sequestration and emission reduction are achieved. In order to achieve the above object, the present invention provides the following technical solutions: the invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative field returning, which comprises the following steps:|The invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative field returning, and belongs to the technical field of soil improvement. The invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative field returning, which comprises the following steps: (1) Crushing common vetch and highland barley straws, mixing the crushed common vetch and highland barley straws with urea and water to obtain a fertilizer to be mixed; (2) stripping the surface soil and digging out core soil; (3) Mixing surface soil and the fertilizer to be mixed, filling the mixture into the position where core soil is dug out, then covering the core soil, and planting crops on the core soil; and (4) repeating the steps (1) to (3) for 1 to 2 times.|The invention relates to the technical field of soil improvement, and particularly relates to a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straw.| (CN115380657)|COMMON VETCH(100,40)|HIGHLAND BARLEY STRAW(100,33)|CARBON SEQUESTRATION(100,21)|EMISSION REDUCTION(100,18)|COMMON VETCH RETURNING(100,6)|COOPERATIVE(100,6)|CARBON FIXATION(100,2)|CORE SOIL(23,16)|PLANTED CROP(23,4)|DIGGING CORE SOIL(16,3)|FERTILIZER(15,20)|FARMLAND INSTALLATION(12,1)|CRUSHED COMMON VETCH(11,5)|LAND UTILIZATION MODE(11,1)|GROUND(10,21)|SOIL IMPROVEMENT(10,3)|SOIL CARBON SEQUESTRATION CAPACITY(10,2)|SOIL CARBON FIXATION CAPACITY(9,1)|COLLABORATIVE FIELD(8,4)|UREA(7,9)|CARBON SEQUESTRATION CAPACITY(7,2)|GRASSLAND(7,2)|FOREST(6,2)|GRINDING PARTICLE SIZE(5,2)|CROP(4,5)|MIXING SURFACE SOIL(4,4)|CARBON EMISSION(4,1)|CARBON SEQUESTRATION EMISSION REDUCTION(4,1)|MOJIAZHU FARM COLLEGE(4,1)|TOPSOIL VOLUME RATIO(4,1)|DEPTH RANGE(3,8)|DIGGING OUT CORE SOIL(3,2)|GRINDING GRANULARITY(3,2)|ORGANIC CARBON(3,1)|STRIPPING SURFACE SOIL(2,5)|COMMON VETCH MASS RATIO(2,2)|GRINDING MESH(2,2)|CRUSHING GRANULARITY(2,1)|FERTILIZATION MANAGEMENT(2,1)|HARVESTED VICIA SATIVA(2,1)|INSTALLED HIGHLAND BARLEY(2,1)|PROTECTIVE FARMING(2,1)|QINGHAI PROVINCE(2,1)|SOIL IMPROPER UTILIZATION(2,1)|SOIL RESTORATION MEASURE(2,1)|UNTIMELY MECHANICAL PLOWING(2,1)|WETLAND DRAINAGE(2,1)|XINING CITY(2,1)|BACKFILLING(1,3)|MOWING(1,3)|COMMON VETCH PLANT(1,2)|COMPACTING(1,2)|DECORATING(1,2)|SEED(1,2)|SOIL STRUCTURE(1,2)|CARBON SUPPLEMENTING(1,1)|CONTRAST SOIL(1,1)|FARMING MACHINE(1,1)|FILLING INTERACTION(1,1)|IMPROPER UTILIZATION MODE(1,1)|INSTALLED MENDING CARBON(1,1)|INTERMITTENT RETURNING MODE(1,1)|MANUAL ADOPTION(1,1)|STEADY TENDENCY(1,1)|TREATED SOILS(1,1)| (CN115380657)|1. A carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straw to field is characterized by comprising the following steps:|(1) Crushing common vetch and highland barley straws, mixing the crushed common vetch and highland barley straws with urea and water to obtain a fertilizer to be mixed;|(2) Stripping surface soil and digging core soil;|(3) Mixing surface soil and the fertilizer to be mixed, filling the mixture into the position where core soil is dug out, then covering the core soil, and planting crops on the core soil;|(4) Repeating the steps (1) to (3) for 1 to 2 times.|2. The carbon sequestration and emission reduction method as claimed in claim 1, wherein the common vetch has a grinding particle size of 50-70 meshes, and the highland barley straw has a grinding particle size of 80-120 meshes.|3. The carbon sequestration and emission reduction method of claim 2, wherein the mass ratio of common vetch, highland barley straw, urea and water is 10-12: 4 to 6:1 to 3:2 to 4.|4. The method for carbon sequestration and emission reduction according to claim 3, wherein the topsoil is soil within a depth range of 15-20 cm from the ground surface.|5. The method for carbon sequestration and emission reduction according to claim 4, wherein the core soil is soil within a depth range of 15-20 cm below the topsoil.|6. The method for carbon sequestration and emission reduction according to claim 5, wherein the volume ratio of the top soil to the fertilizer to be mixed is 3-5: 1 to 2.|7. The method for carbon sequestration and emission reduction according to claim 6, wherein the crop is vicia sativa and/or highland barley.|8. The method for carbon sequestration emission reduction according to any one of claims 1 to 7, wherein in the step (4), the time interval for repeating the steps (1) to (3) is 1 to 2 years. (CN115380657)|TECHNICAL FIELD|[0001] The invention relates to the technical field of soil improvement, and particularly relates to a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straw.|BACKGROUND ART|[0002] The soil is degraded due to the utilization and the improper utilization of the soil by human beings, so that the carbon fixing capacity of the soil is further reduced, the emission of carbon dioxide in the atmosphere is increased, and the global warming is aggravated. Research shows that the change of land utilization modes from grassland and forest land to farmland can cause the loss of organic carbon in soil. Improper utilization modes, such as excessive plowing, wetland drainage, low water resource management, excessive and untimely mechanical plowing, no-input or low-input production and the like, can also cause the reduction of the organic matter content of the soil and accelerate the soil degradation. On the contrary, the soil restoration measures can increase the organic carbon content of the soil, restore the soil fertility and relieve the greenhouse effect. These include the use of protective farming techniques, the restoration of severely degraded land to grasslands and forests, the application of organic materials, crop rotation, improved machine farming, irrigation, and the like. Therefore, it is necessary to improve and scientifically and reasonably utilize the soil and improve the carbon sequestration capacity of the soil.|DISCLOSURE|Disclosure of Invention|[0003] The invention aims to provide a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straws to field, and the purposes of soil improvement and carbon sequestration and emission reduction are achieved.|[0004] In order to achieve the above object, the present invention provides the following technical solutions:|[0005] the invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative field returning, which comprises the following steps:|[0006] (1) Crushing common vetch and highland barley straws, mixing the crushed common vetch and highland barley straws with urea and water to obtain a fertilizer to be mixed;|[0007] (2) Stripping surface soil and digging core soil;|[0008] (3) Mixing surface soil and the fertilizer to be mixed, filling the mixture into the position where core soil is dug out, then covering the core soil, and planting crops on the core soil;|[0009] (4) Repeating the steps (1) to (3) for 1 to 2 times.|[0010] Preferably, the grinding granularity of the common vetch is 50-70 meshes, and the grinding granularity of the highland barley straws is 80-120 meshes.|[0011] Preferably, the mass ratio of the common vetch to the highland barley straws to the urea to the water is 10-12: 4 to 6:1 to 3:2 to 4.|[0012] Preferably, the top soil is soil within a depth range of 15 to 20cm from the surface of the earth.|[0013] Preferably, the core soil is soil within a depth range of 15 to 20cm below the surface soil.|[0014] Preferably, the volume ratio of the surface soil to the fertilizer to be mixed is 3-5: 1 to 2.|[0015] Preferably, the crop is vicia sativa and/or highland barley.|[0016] Preferably, in the step (4), the time interval for repeating the steps (1) to (3) is 1 to 2 years.|[0017] The invention provides a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straws to field.|INVENTION MODE|Detailed Description|[0018] The invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative field returning, which comprises the following steps:|[0019] (1) Crushing common vetch and highland barley straws, mixing the crushed common vetch and highland barley straws with urea and water to obtain a fertilizer to be mixed;|[0020] (2) Stripping surface soil and digging core soil;|[0021] (3) Mixing surface soil and the fertilizer to be mixed, filling the mixture into the position where core soil is dug out, then covering the core soil, and planting crops on the core soil;|[0022] (4) Repeating the steps (1) to (3) for 1 to 2 times.|[0023] In the present invention, common vetch is preferably a fresh whole plant of common vetch, and highland barley straw is preferably fresh straw of highland barley.|[0024] In the present invention, the ground particle size of common vetch is 50 to 70 mesh, preferably 60 mesh.|[0025] In the invention, the crushing granularity of the highland barley straws is 80-120 meshes, and preferably 100 meshes.|[0026] In the invention, the mass ratio of common vetch to common oat, highland barley straw to urea to water is 10-12: 4 to 6:1 to 3:2 to 4, preferably 10:5:2:3.|[0027] in the present invention, the top soil is soil within a depth range of 15 to 20cm from the surface of the earth, and preferably within a depth range of 20cm from the surface of the earth.|[0028] In the present invention, the core soil is a soil within a depth range of 15 to 20cm below the surface soil, and preferably a soil within a depth range of 20cm below the surface soil.|[0029] In the invention, the volume ratio of the surface soil to the fertilizer to be mixed is 3-5: 1 to 2, and more preferably 3:1.|[0030] In the present invention, the crop is vicia sativa and/or highland barley, preferably vicia sativa and highland barley. When the crop is vicia sativa and highland barley, the planting area ratio of vicia sativa to highland barley is preferably 5-7:3, and more preferably 5:3. The harvested vicia sativa and highland barley may be used to return to the field.|[0031] In the present invention, the number of times of repeating the steps (1) to (3) is preferably 2 times.|[0032] In the present invention, the time interval for repeating the steps (1) to (3) is 1 to 2 years, preferably 2 years.|[0033] The technical solutions provided by the present invention are described in detail below with reference to examples, but they should not be construed as limiting the scope of the present invention.|[0034] Example 1|[0035] The experiment is carried out in a Mojiazhu farm college of Twen, xining City, qinghai province, and the experiment time is 2017 to 2021 years.|[0036] The variety of common vetch used for the test is Ximu 324, and the variety of highland barley is Kunlun No. 15.|[0037] And (4) cutting common vetch and highland barley (planted in 2017 in 4 months) in 7 months in 2017 for later use.|[0038] Smashing the whole common vetch plant, sieving with a 60-mesh sieve, taking undersize, smashing highland barley straw, sieving with a 100-mesh sieve, and taking undersize. Mixing the crushed common vetch and highland barley straw with urea and water according to a mass ratio of 10:5:2:3, uniformly mixing to obtain the fertilizer to be mixed for later use.|[0039] The area of the test field is 500 square meters, and the test field is divided into 5 test areas, and each test area is 100 square meters.|[0040] One area was designated as control 1, without any treatment, only in 4 months per year, with the area ratio of 5:3 common vetch and highland barley sown, and mown in 7 months.|[0041] Taking the second area as a comparison 2, deeply ploughing the land in 4 months of 2017-2020, wherein the deep ploughing depth is 20cm, then sowing common vetch and highland barley in 4 months of each year according to the area ratio of 5:3, and mowing in 7 months.|[0042] And taking the three zones as test 1, taking soil stripped at the depth of 0-20 cm in 7 months in 2017 as surface soil, digging out soil at the depth of 20-40 cm as core soil, uniformly mixing the surface soil and the fertilizer to be mixed according to the volume ratio of 3:1, filling the mixture into the position where the core soil is dug out, then covering the position with the core soil, and compacting. The vicia sativa and the highland barley were sown in an area ratio of 5:3 in 4 months of 2018. After harvesting in 2018, the seeds are not treated. And continuously sowing common vetch and highland barley in the area ratio of 5:3 in 2019 in 4 months, after mowing, preparing the fertilizer to be mixed according to the method in 2017, mixing the fertilizer with surface soil, backfilling, covering with core soil, compacting, and mowing in 2019 in 7 months. No treatment was performed in 2020.|[0043] The four areas are taken as a test 2, and the modes of preparing the fertilizer to be mixed, stripping surface soil, digging out core soil and backfilling are the same as the test 1, and the difference is that the fertilizer is treated every year from 2017 to 2020.|[0044] The five areas are taken as a test 3, the modes and the processing time for preparing the stripping surface soil, digging out the core soil and backfilling are the same as those of the test 1, and the difference is that when the fertilizer to be mixed is prepared, the grinding mesh number of common vetch is 100 meshes, and the grinding mesh number of highland barley straws is 60 meshes.|[0045] The method for sowing common vetch and highland barley in the test and the fertilization management are as follows: adopting manual ditching and drilling, the row spacing is 35cm, and the seeding depth is 5cm. Applying 1.5kg/100m urea before sowing 2 Diammonium phosphate 1kg/100m 2 The fertilizer is used as a base fertilizer, does not need additional fertilizer and can weed in time.|[0046] The tests are respectively carried out on the soil carbon content in the 4 months of each year from 2017 to 2020. When sampling, selecting 0-20 cm soil. The carbon content was expressed as Total Organic Carbon (TOC) content and was measured using a total organic carbon analyzer. The results are shown in Table 1.|[0047] TABLE 1 variation of carbon content in different treated soils|[0048] |[0049] As can be seen from table 1, control 1 shows a steady tendency of a slow increase in the total organic carbon content in the soil when only the crop is planted without any land treatment. Compared with the control 2, under the condition of adding deep ploughing treatment to the soil, the carbon loss is serious, because organic matters are exposed and easily lost under the condition of only carrying out deep ploughing treatment, and meanwhile, the soil structure is damaged by deep ploughing in successive years, the carbon sequestration capacity of the soil is reduced, and finally, the organic carbon loss of the soil is serious.|[0050] The result of the test 1 shows that the carbon sequestration effect is obvious by the method for cooperatively returning the common vetch and the highland barley straw to the field. Experimental difference of comparing in 1 lies in adopting common vetch and highland barley straw to return to the field in coordination 4 years in the adoption, though compare in 1 soil of contrast and increase in total organic carbon content, but it drops into under the more circumstances of organic matter than 1 of contrast and experiment 1, but does not reach the effect that experiment 1 is even better than experiment 1, consequently, think that returning to the field in succession is favorable to mending carbon, but does not have better solid carbon effect. Therefore, the land can be more reasonably utilized by adopting an intermittent returning mode. Experiment 3 after the grain size of common vetch and highland barley straw is changed, the carbon sequestration effect is reduced compared with experiment 1, the main reason is that the texture and grain size of green manure are related to the effect of improving soil, and organic matter has the effect of supplementing carbon source and also has the interaction of physical filling, chemical decomposition, biological conversion and the like after being applied into soil. Under the action, the carbon supplementing effect and the carbon fixing effect are different due to the fact that different organic matters are added in different particle sizes.|[0051] According to the embodiment, the carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straws is provided.|[0052] The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention. (CN115380657)|TECHNICAL FIELD|[0001] The invention relates to the technical field of soil improvement, and particularly relates to a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straw.|BACKGROUND ART|[0002] The soil is degraded due to the utilization and the improper utilization of the soil by human beings, so that the carbon fixing capacity of the soil is further reduced, the emission of carbon dioxide in the atmosphere is increased, and the global warming is aggravated. Research shows that the change of land utilization modes from grassland and forest land to farmland can cause the loss of organic carbon in soil. Improper utilization modes, such as excessive plowing, wetland drainage, low water resource management, excessive and untimely mechanical plowing, no-input or low-input production and the like, can also cause the reduction of the organic matter content of the soil and accelerate the soil degradation. On the contrary, the soil restoration measures can increase the organic carbon content of the soil, restore the soil fertility and relieve the greenhouse effect. These include the use of protective farming techniques, the restoration of severely degraded land to grasslands and forests, the application of organic materials, crop rotation, improved machine farming, irrigation, and the like. Therefore, it is necessary to improve and scientifically and reasonably utilize the soil and improve the carbon sequestration capacity of the soil.|DISCLOSURE|Disclosure of Invention|[0003] The invention aims to provide a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straws to field, and the purposes of soil improvement and carbon sequestration and emission reduction are achieved.|[0004] In order to achieve the above object, the present invention provides the following technical solutions:|[0005] the invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative field returning, which comprises the following steps:|[0006] (1) Crushing common vetch and highland barley straws, mixing the crushed common vetch and highland barley straws with urea and water to obtain a fertilizer to be mixed;|[0007] (2) Stripping surface soil and digging core soil;|[0008] (3) Mixing surface soil and the fertilizer to be mixed, filling the mixture into the position where core soil is dug out, then covering the core soil, and planting crops on the core soil;|[0009] (4) Repeating the steps (1) to (3) for 1 to 2 times.|[0010] Preferably, the grinding granularity of the common vetch is 50-70 meshes, and the grinding granularity of the highland barley straws is 80-120 meshes.|[0011] Preferably, the mass ratio of the common vetch to the highland barley straws to the urea to the water is 10-12: 4 to 6:1 to 3:2 to 4.|[0012] Preferably, the top soil is soil within a depth range of 15 to 20cm from the surface of the earth.|[0013] Preferably, the core soil is soil within a depth range of 15 to 20cm below the surface soil.|[0014] Preferably, the volume ratio of the surface soil to the fertilizer to be mixed is 3-5: 1 to 2.|[0015] Preferably, the crop is vicia sativa and/or highland barley.|[0016] Preferably, in the step (4), the time interval for repeating the steps (1) to (3) is 1 to 2 years.|[0017] The invention provides a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straws to field.|INVENTION MODE|Detailed Description|[0018] The invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative field returning, which comprises the following steps:|[0019] (1) Crushing common vetch and highland barley straws, mixing the crushed common vetch and highland barley straws with urea and water to obtain a fertilizer to be mixed;|[0020] (2) Stripping surface soil and digging core soil;|[0021] (3) Mixing surface soil and the fertilizer to be mixed, filling the mixture into the position where core soil is dug out, then covering the core soil, and planting crops on the core soil;|[0022] (4) Repeating the steps (1) to (3) for 1 to 2 times.|[0023] In the present invention, common vetch is preferably a fresh whole plant of common vetch, and highland barley straw is preferably fresh straw of highland barley.|[0024] In the present invention, the ground particle size of common vetch is 50 to 70 mesh, preferably 60 mesh.|[0025] In the invention, the crushing granularity of the highland barley straws is 80-120 meshes, and preferably 100 meshes.|[0026] In the invention, the mass ratio of common vetch to common oat, highland barley straw to urea to water is 10-12: 4 to 6:1 to 3:2 to 4, preferably 10:5:2:3.|[0027] in the present invention, the top soil is soil within a depth range of 15 to 20cm from the surface of the earth, and preferably within a depth range of 20cm from the surface of the earth.|[0028] In the present invention, the core soil is a soil within a depth range of 15 to 20cm below the surface soil, and preferably a soil within a depth range of 20cm below the surface soil.|[0029] In the invention, the volume ratio of the surface soil to the fertilizer to be mixed is 3-5: 1 to 2, and more preferably 3:1.|[0030] In the present invention, the crop is vicia sativa and/or highland barley, preferably vicia sativa and highland barley. When the crop is vicia sativa and highland barley, the planting area ratio of vicia sativa to highland barley is preferably 5-7:3, and more preferably 5:3. The harvested vicia sativa and highland barley may be used to return to the field.|[0031] In the present invention, the number of times of repeating the steps (1) to (3) is preferably 2 times.|[0032] In the present invention, the time interval for repeating the steps (1) to (3) is 1 to 2 years, preferably 2 years.|[0033] The technical solutions provided by the present invention are described in detail below with reference to examples, but they should not be construed as limiting the scope of the present invention.|[0034] Example 1|[0035] The experiment is carried out in a Mojiazhu farm college of Twen, xining City, qinghai province, and the experiment time is 2017 to 2021 years.|[0036] The variety of common vetch used for the test is Ximu 324, and the variety of highland barley is Kunlun No. 15.|[0037] And (4) cutting common vetch and highland barley (planted in 2017 in 4 months) in 7 months in 2017 for later use.|[0038] Smashing the whole common vetch plant, sieving with a 60-mesh sieve, taking undersize, smashing highland barley straw, sieving with a 100-mesh sieve, and taking undersize. Mixing the crushed common vetch and highland barley straw with urea and water according to a mass ratio of 10:5:2:3, uniformly mixing to obtain the fertilizer to be mixed for later use.|[0039] The area of the test field is 500 square meters, and the test field is divided into 5 test areas, and each test area is 100 square meters.|[0040] One area was designated as control 1, without any treatment, only in 4 months per year, with the area ratio of 5:3 common vetch and highland barley sown, and mown in 7 months.|[0041] Taking the second area as a comparison 2, deeply ploughing the land in 4 months of 2017-2020, wherein the deep ploughing depth is 20cm, then sowing common vetch and highland barley in 4 months of each year according to the area ratio of 5:3, and mowing in 7 months.|[0042] And taking the three zones as test 1, taking soil stripped at the depth of 0-20 cm in 7 months in 2017 as surface soil, digging out soil at the depth of 20-40 cm as core soil, uniformly mixing the surface soil and the fertilizer to be mixed according to the volume ratio of 3:1, filling the mixture into the position where the core soil is dug out, then covering the position with the core soil, and compacting. The vicia sativa and the highland barley were sown in an area ratio of 5:3 in 4 months of 2018. After harvesting in 2018, the seeds are not treated. And continuously sowing common vetch and highland barley in the area ratio of 5:3 in 2019 in 4 months, after mowing, preparing the fertilizer to be mixed according to the method in 2017, mixing the fertilizer with surface soil, backfilling, covering with core soil, compacting, and mowing in 2019 in 7 months. No treatment was performed in 2020.|[0043] The four areas are taken as a test 2, and the modes of preparing the fertilizer to be mixed, stripping surface soil, digging out core soil and backfilling are the same as the test 1, and the difference is that the fertilizer is treated every year from 2017 to 2020.|[0044] The five areas are taken as a test 3, the modes and the processing time for preparing the stripping surface soil, digging out the core soil and backfilling are the same as those of the test 1, and the difference is that when the fertilizer to be mixed is prepared, the grinding mesh number of common vetch is 100 meshes, and the grinding mesh number of highland barley straws is 60 meshes.|[0045] The method for sowing common vetch and highland barley in the test and the fertilization management are as follows: adopting manual ditching and drilling, the row spacing is 35cm, and the seeding depth is 5cm. Applying 1.5kg/100m urea before sowing 2 Diammonium phosphate 1kg/100m 2 The fertilizer is used as a base fertilizer, does not need additional fertilizer and can weed in time.|[0046] The tests are respectively carried out on the soil carbon content in the 4 months of each year from 2017 to 2020. When sampling, selecting 0-20 cm soil. The carbon content was expressed as Total Organic Carbon (TOC) content and was measured using a total organic carbon analyzer. The results are shown in Table 1.|[0047] TABLE 1 variation of carbon content in different treated soils|[0048] |[0049] As can be seen from table 1, control 1 shows a steady tendency of a slow increase in the total organic carbon content in the soil when only the crop is planted without any land treatment. Compared with the control 2, under the condition of adding deep ploughing treatment to the soil, the carbon loss is serious, because organic matters are exposed and easily lost under the condition of only carrying out deep ploughing treatment, and meanwhile, the soil structure is damaged by deep ploughing in successive years, the carbon sequestration capacity of the soil is reduced, and finally, the organic carbon loss of the soil is serious.|[0050] The result of the test 1 shows that the carbon sequestration effect is obvious by the method for cooperatively returning the common vetch and the highland barley straw to the field. Experimental difference of comparing in 1 lies in adopting common vetch and highland barley straw to return to the field in coordination 4 years in the adoption, though compare in 1 soil of contrast and increase in total organic carbon content, but it drops into under the more circumstances of organic matter than 1 of contrast and experiment 1, but does not reach the effect that experiment 1 is even better than experiment 1, consequently, think that returning to the field in succession is favorable to mending carbon, but does not have better solid carbon effect. Therefore, the land can be more reasonably utilized by adopting an intermittent returning mode. Experiment 3 after the grain size of common vetch and highland barley straw is changed, the carbon sequestration effect is reduced compared with experiment 1, the main reason is that the texture and grain size of green manure are related to the effect of improving soil, and organic matter has the effect of supplementing carbon source and also has the interaction of physical filling, chemical decomposition, biological conversion and the like after being applied into soil. Under the action, the carbon supplementing effect and the carbon fixing effect are different due to the fact that different organic matters are added in different particle sizes.|[0051] According to the embodiment, the carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straws is provided.|[0052] The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention. Family Number|(102741067)|102741067|Abstract|(CN115380657 A)|The invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative returning , and belongs to the technical field of soil improvement . The invention provides a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straw , which comprises the following steps : ( 1 ) crushing common vetch and highland barley straw , and mixing with urea and water to obtain a to - be - mixed fertilizer ; ( 2 ) surface soil is stripped , and core soil is dug out ; ( 3 ) mixing surface soil with a to - be - mixed fertilizer , filling the mixture into the position where the core soil is dug out , then covering the core soil , and planting crops on the core soil ; and ( 4 ) repeating the steps ( 1 ) - ( 3 ) for 1-2 times . According to the method , the common vetch straw and the highland barley straw are cooperatively returned to the field , the soil structure is improved in the mode that surface soil and core soil are alternately fertilized at intervals , a carbon source is supplemented , the carbon sequestration capacity of the soil is improved , and carbon emission is reduced . |CPC codes|(CN115380657 A)|A01B - 079/02 |IPC codes|(CN115380657 A)|A01B - 079/02 |Title|(CN115380657 A)|Carbon sequestration and emission reduction method based on cooperative returning of vicia sativa and highland barley straw to field | Other special machines A01B-079/02 A01B-079/02 A01B-079/02 A01B-079/02 CN117326896B CN117326896B 108008755 WHO=Examiner SELF=N CN112492916|CN114711008|CN112616351|CN109566308|RU2095955 CN112492916 93149148 WHO=Examiner SELF=N CAT=Y|CN114711008 100809367 WHO=Examiner SELF=N CAT=A|CN112616351 93531001 WHO=Examiner SELF=N CAT=A|CN109566308 84068517 WHO=Examiner SELF=N CAT=A|RU2095955 36083033 WHO=Examiner SELF=N CAT=A 李正鹏 等: &quot;青藏高原小麦秸秆和箭筈豌豆混合腐解规律和养分释放特征&quot;, 农 业 工 程 学 报, vol. 37, no. 11 (Cat. Y) RU2095955; CN109566308; CN112492916; CN112616351; CN114711008 REVOKED (CN115380657)|REVOKED DEAD (CN115380657)|DEAD (CN115380657)|LEGAL DETAILS FOR CN115380657|Actual or expected expiration date=2024-09-17|Legal state=DEAD|Status=REVOKED|Event publication date=2022-09-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211191239|Application date=2022-09-28|Standardized application number=2022CN-1191239|Event publication date=2022-11-25|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115380657|Publication stage code=A|Publication date=2022-11-25|Standardized publication number=CN115380657|Event publication date=2022-11-25|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-12-13|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-09-17|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTKWARfp8Uju1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000065605638&ekey=2121&xpn=CN115380657&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=nc1QSOZ4BFdBi5NsJqiS%252B5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN115380657)|CN (CN115380657)|NAME=QINGHAI ACADEMY OF AGRICULTURAL & FORESTRY , COUNTRY=CN (CN115380657)|NAME=DONG DAYUAN;RZBC PATENT AGENCY (GENERAL PARTNERSHIP) , REG=11732 (CN115380657)|NAME=HAN MEI|NAME=LI ZHENGPENG 0 1 Titre: (CN115380657)|Carbon sequestration and emission reduction method based on cooperative returning of vicia sativa and highland barley straw to field Résumé: (CN115380657)|The invention provides a carbon sequestration and emission reduction method based on common vetch and highland barley straw collaborative returning, and belongs to the technical field of soil improvement. The invention provides a carbon sequestration and emission reduction method based on cooperative returning of common vetch and highland barley straw, which comprises the following steps: (1) crushing common vetch and highland barley straw, and mixing with urea and water to obtain a to-be-mixed fertilizer; (2) surface soil is stripped, and core soil is dug out; (3) mixing surface soil with a to-be-mixed fertilizer, filling the mixture into the position where the core soil is dug out, then covering the core soil, and planting crops on the core soil; and (4) repeating the steps (1)-(3) for 1-2 times. According to the method, the common vetch straw and the highland barley straw are cooperatively returned to the field, the soil structure is improved in the mode that surface soil and core soil are alternately fertilized at intervals, a carbon source is supplemented, the carbon sequestration capacity of the soil is improved, and carbon emission is reduced. 25 Abstract gpt-4o-mini no The article focuses on a method involving organic materials (straw) and soil improvement for carbon sequestration, without addressing mineral weathering or CO₂ capture through mineral carbonation.
32 CN202210599827 CN202210599827 CN115069362|CN115069362 101844296 CN115069362 B 2023-11-21 [CN115069362B]|CN115069362 A 2022-09-20 [CN115069362] 2022-05-30 2022-05-30 2023-11-21|2022-09-20 (CN115069362B)|2023-11-21 (CN115069362)|2042-05-30 (CN115069362)|Method for carbon fixation and emission reduction of wet-milling steel slag in steel plant and application of method (CN115069362)|The invention discloses a steel plant wet grinding steel slag carbon sequestration and emission reduction method, which comprises: (1) carrying out water quenching and quenching on molten steel slag produced by a steel plant, and sequentially carrying out crushing, iron removal and dry grinding to obtain steel slag powder with a median particle size of 20-500 [mu] m; (2) mixing the steel slag powder and water according to a mass ratio of 1: (1-4), and stirring to obtain steel slag slurry; (3) collecting CO2-containing flue gas discharged by the steel plant into a gas collection bottle; (4) introducing 100 parts by mass of the steel slag slurry and 5-18 parts by mass of flue gas into a horizontal stirring ball mill, adding a grinding medium and a stabilizer accounting for 1-5% of the mass of the steel slag powder for wet grinding, and fixing carbon by using the steel slag slurry; and (5) drying the wet-ground slurry to obtain the CO2 curing material. The method has the advantages of high carbon sequestration rate, low cost and environmental protection, and is suitable for popularization and production. HUBEI UNIVERSITY OF TECHNOLOGY (CN115069362)|HUBEI UNIVERSITY OF TECHNOLOGY ([CN])|(CN115069362)|HUBEI UNIVERSITY OF TECHNOLOGY ([CN]) SU YING|LI CHENGHAO|HE XINGYANG|ZHENG ZHENGQI|YANG JIN|WANG YINGBIN|TAN HONGBO (CN115069362)|SU YING|LI CHENGHAO|HE XINGYANG|ZHENG ZHENGQI|YANG JIN|WANG YINGBIN|TAN HONGBO|(CN115069362)|SU YING|LI CHENGHAO|HE XINGYANG|ZHENG ZHENGQI|YANG JIN|WANG YINGBIN|TAN HONGBO (CN115069362)|WANG DONGDONG;WUHAN SINOPOWER PATENT AGENCY|Reg. Nb: 42237 (CN115069362)|In summary, the method provided by the invention has the advantages of high carbon fixation rate, low cost and environmental friendliness, and is suitable for popularization and production.|In the Chinese patent publication No. CN 104860474A, a method for fixing carbon and biologically treating sulfur-containing waste lye is disclosed, which uses biotechnology, needs to culture anaerobic bacteria special for fixing carbon, and needs to use strong alkali sodium hydroxide in a plurality of procedures, and has the advantages of complex process, difficult control, high cost and low carbon fixing rate.|In summary, the existing carbon fixing method generally has the problem that the carbon fixing rate and the cost are difficult to be compatible, and the waste gas and the waste liquid of most carbon fixing methods are not beneficial to environmental protection.|Taking into account CO 2 The solidification reaction occurs in an alkaline environment, and a large amount of alkaline steel slag generated by a steel plant is used for CO 2 Has great potential and prospect in curing and sealing, but the prior method for fixing carbon by utilizing steel slag has the difficult problem which is partially difficult to solve.|The agglomeration phenomenon of steel slag particles easily occurs when steel slag is pulped, and the coated steel slag particles are difficult to contact CO 2 The method comprises the steps of carrying out a first treatment on the surface of the In the carbon fixation reaction process, calcium and magnesium ions in the steel slag particles can slowly dissolve out, and in the calcium and magnesium ion dissolution process, siliceous film structures can be generated in the steel slag particles to prevent the calcium and magnesium ions from continuously dissolving out.| (CN115069362)|1. A method for carbon fixation and emission reduction of wet-milling steel slag in a steel plant is characterized by comprising the following steps:(1) Quenching molten steel slag produced by a steel plant in a water quenching way, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with a median particle size of 20-500 mu m;(2) The steel slag powder and water are mixed according to the mass ratio of 1: (1-4) mixing and stirring to obtain steel slag slurry;(3) CO-containing effluent from steel plants 2 The flue gas is collected in a gas collecting bottle;(4) Introducing 100 parts by mass of steel slag slurry and 5-18 parts by mass of flue gas into a horizontal stirred ball mill, adding grinding media and a stabilizer accounting for 1-5% of the mass of steel slag powder for wet grinding, and carrying out carbon fixation by utilizing the steel slag slurry;(5) Drying the wet ground slurry to obtain CO 2 Solidifying the material;the stabilizer adopts one or a combination of more of sucrose, sodium gluconate, sodium citrate and sodium metaphosphate; the grinding medium is used in an amount of 50-100 parts by mass.| (CN115069362)|The invention aims to provide a method for carbon sequestration and emission reduction of wet-milled steel slag in a steel plant and application thereof, wherein the method has obviously higher reaction efficiency and carbon sequestration rate.|The invention discloses a method for carbon fixation and emission reduction of wet-milling steel slag in a steel plant, which comprises the following steps: (1) Quenching molten steel slag produced by a steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with the median particle size of 20-500 mu m; (2) mixing steel slag powder and water according to a mass ratio of 1: (1-4) mixing and stirring to obtain steel slag slurry; (3) CO-containing effluent from steel plants 2 The flue gas is collected in a gas collecting bottle; (4) Introducing 100 parts by mass of steel slag slurry and 5-18 parts by mass of flue gas into a horizontal stirred ball mill, adding grinding media and a stabilizer accounting for 1-5% of the mass of steel slag powder for wet grinding, and carrying out carbon fixation by utilizing the steel slag slurry; (5) Drying the wet ground slurry to obtain CO 2 And curing the material.| (CN115069362)|STEEL SLAG SLURRY(100,46)|STEEL SLAG(100,41)|CARBON FIXATION(100,35)|STEEL PLANT(100,32)|EMISSION REDUCTION(100,11)|WET MILLING(100,10)|WET MILLING STEEL SLAG(100,4)|COCONTAINING EFFLUENT(99,3)|STABILIZER ACCOUNTING(89,5)|STEEL SLAG POWDER(80,13)|WET MILLED STEEL SLAG(70,5)|WET SOIL SLURRY(59,3)|MOLTEN STEEL SLAG(56,9)|AGGLOMERATION PHENOMENON(56,1)|GRINDING MEDIA ADDITION(55,3)|CULTURE ANAEROBIC BACTERIUM(55,1)|STEEL SLAG PARTICLE(54,16)|ALKALINE STEEL SLAG(53,1)|FIXING CARBON(49,3)|GAS COLLECTION BOTTLE(47,11)|SPHERICAL DIAMETER(45,6)|SULFUR TREATMENT(44,1)|SLAG PARTICLE(43,1)|WASTE LYE(43,1)|GRINDING MEDIUM(41,11)|WET GRINDING(41,11)|COATED STEEL SLAG PARTICLE(41,1)|POPULARIZATION(40,2)|CARBON SEQUESTRATION(39,7)|FRIENDLINESS(38,1)|OVERFLOWED GAS(37,6)|MAGNESIUM ION(34,6)|ALKALINE ENVIRONMENT(34,1)|WATER QUENCHING(33,8)|DEIRONING(32,8)|SOLIDIFICATION REACTION(32,2)|ANAEROBIC BACTERIUM(29,1)|CRUSHING(28,8)|ALKALI SODIUM HYDROXIDE(28,1)|BIOTECHNOLOGY(28,1)|AGATE BALL(26,2)|STABILIZER(26,2)|GRINDING(25,20)|ZIRCONIA BALL(25,2)|PROSPECT(25,1)|HORIZONTAL STIRRING BALL MILL(24,28)|CARBON FIXING WASTE LIQUID(23,1)|FUME INTRODUCTION SPEED(22,2)|WET GRINDING SLURRY(22,2)|FLUE GAS(21,26)|SODIUM METAPHOSPHATE(21,2)|DISSOLVE(21,1)|MAGNESIUM ION DISSOLUTION(21,1)|SUITABILITY(21,1)|SUCROSE(20,2)|WASTE LIQUID(20,2)|CARBON SEQUESTRATION RATE(20,1)|SILICEOUS FILM STRUCTURE(20,1)|AVERAGE PARTICLE SIZE(19,9)|CURING(19,1)|PREVENT CALCIUM(19,1)|BALL MILL(18,16)|ENVIRONMENTAL PROTECTION(18,5)|SODIUM CITRATE(17,2)|STEEL WORK(16,4)|SODIUM HYDROXIDE(16,1)|CARBON FIXING(15,6)|SLAG(15,2)|SODIUM GLUCONATE(14,7)|SLURRY SAMPLE(14,6)|GRINDING BALL MASS RATIO(14,2)|CARBON FIXING RATE(14,1)|STEEL SLAG AGGLOMERATION(13,2)|MASS RATIO(12,10)|ABSORPTION TOWER(12,4)|STOPPING(12,2)|LOW COST FRIENDLINESS(12,1)|THERMOGRAVIMETRIC ANALYSIS DATA(11,6)|HUNDRED MILLION TON(11,4)|OBVIOUSLY HIGH REACTION(11,1)|BALL DIAMETER(10,21)|AIR COLLECTION BOTTLE(10,5)|PH TESTER(10,5)|WASTE GAS(10,2)|CARBON FIXATION REACTION(10,1)|GRINDING MEDIA MASS(9,4)|PH DETECTION INSTRUMENT(9,4)|DIFFICULT CONTROL(9,1)|STEEL SLAG ALKALINITY(9,1)|DRIED SAMPLE(8,6)|FEED INLET(8,6)|CARBONATE DECOMPOSITIONRAW(8,1)|QUENCHED STEEL SLAG(8,1)|AERATION(7,5)|SIEVING(7,5)|SODIUM GLUCONATE MASS(7,5)|WET GRINDING(7,5)|STEEL SLAG CARBON FIXATION(7,3)|HIGH CARBON FIXATION RATE(7,2)|MASS CONCENTRATION(7,2)|CALCULATED SAMPLE MASS LOSS(6,4)|SAMPLE CALCULATION(6,4)|SAMPLE OBTAINING MASS LOSS(6,4)|ALKALINE POLLUTION(6,1)|ANNUAL EMISSION(6,1)|DENSE CARBONIZED FILM(6,1)|LOW CARBON FIXING RATE(6,1)|NATURAL DISASTER FREQUENT OCCURRENCE(6,1)|PARTICLE AGGLOMERATION(6,1)|ROLE PROMOTION(6,1)|STEEL SLAG SLURRY PH(6,1)|WET DECARBURIZATION(6,1)|STANDBY(5,6)|FREEZE DRYING(5,5)|ROTATING SPEED(5,5)|AIRTIGHT HORIZONTAL STIRRING BALL(5,1)|ANNUAL DISCHARGE(5,1)|CONSUMPTION STATE(5,1)|ECOLOGICAL ENVIRONMENT(5,1)|ECONOMIC BENEFIT(5,1)|GLOBAL COARSE STEEL YIELD(5,1)|MILLING MEDIA(5,1)|WET GRINDING STEEL SLAG(5,1)|AMMONIUM BICARBONATE SOLUTION(4,2)|PH DETECTOR(4,2)|REGULAR TIME(4,2)|SILICEOUS INNER MEMBRANE(4,2)|ACTIVE INGREDIENT(4,1)|AVERAGE PARTICLE DIAMETER(4,1)|CALCIUM CARBONATE CARBONIZED FILM(4,1)|CALCIUM CARBONATE PRECIPITATE(4,1)|CARBONIZATION(4,1)|GAS COLLECTION CYLINDER(4,1)|GRINDING MEDIUM MASS(4,1)||(CN115069362)|CARBON FIXATION(100,36)|STEEL PLANT(100,36)|EMISSION REDUCTION(100,14)|WET GRINDING STEEL SLAG(100,3)|STEEL SLAG SLURRY(99,47)|STEEL SLAG POWDER(80,13)|WET MILLED STEEL SLAG(79,10)|STABILIZER ACCOUNTING(62,4)|STEEL SLAG(56,39)|MOLTEN STEEL SLAG(56,9)|CARBON SEQUESTRATION(55,19)|AGGLOMERATION PHENOMENON(55,1)|STEEL SLAG PARTICLE(53,17)|MAGNESIUM ION DISSOLUTION(51,1)|GRINDING MEDIUM(49,20)|GAS COLLECTION BOTTLE(46,12)|WET GRINDING(44,9)|GRINDING BALL GRADING(43,1)|SLAG PARTICLE(43,1)|STIRRING BALL MILL(41,39)|COATED STEEL SLAG PARTICLE(41,1)|HORIZONTAL STIRRING BALL MILL(40,38)|POPULARIZATION(40,2)|MAGNESIUM ION(34,6)|ALKALINE ENVIRONMENT(34,1)|SUITABILITY(33,2)|OVERFLOW GAS(32,7)|STABILIZER(32,3)|CURING REACTION(31,1)|GRINDING MEDIUM DOSAGE(31,1)|SOLIDIFICATION(30,1)|BALL DIAMETER(27,27)|SLURRY(25,18)|AGATE BALL(25,2)|PROSPECT(25,1)|ENVIRONMENTAL PROTECTION(24,6)|ZIRCONIA BALL(24,2)|FLUE GAS(23,32)|IRON REMOVAL(23,3)|DEIRONING(21,5)|WET GRINDING SLURRY(21,2)|WATER QUENCHING(20,5)|GRINDING(19,14)|AVERAGE PARTICLE SIZE(19,9)|PREVENT CALCIUM(19,1)|STEEL WORK(16,3)|CARBON SEQUESTRATION RATE(16,2)|CARBONATE DECOMPOSITION(14,6)|GRINDING BALL MASS RATIO(14,2)|THERMOGRAVIMETRIC ANALYSIS TEST(13,6)|SLAG(13,3)|SLURRY SAMPLE(12,5)|ABSORPTION TOWER(12,4)|SODIUM METAPHOSPHATE(12,2)|SUCROSE(12,2)|CARBON SEQUESTRATION REACTION(12,1)|SILICEOUS INCREASE STRUCTURE(12,1)|MASS RATIO(11,10)|THERMOGRAVIMETRIC ANALYSIS DATA(11,6)|STEEL SLAG SLURRY MINERALIZATION(11,1)|ROTATING SPEED(10,6)|GRINDING MEDIUM MASS(10,5)|PH TESTER(10,5)|SODIUM CITRATE(10,2)|WASTE GAS(10,2)|AIR COLLECTION BOTTLE(9,4)|PH DETECTION INSTRUMENT(9,4)|ANNUAL EMISSION(9,2)|STEEL SLAG ALKALINITY(9,1)|DRIED SAMPLE(8,6)|GRINDING MEDIA(8,3)|MASS LOSS(7,12)|WET GRINDING(7,6)|AERATION(7,5)|SIEVING(7,5)|SODIUM GLUCONATE MASS(7,5)|STEEL SLAG CARBON FIXATION(7,3)|HIGH CARBON FIXATION RATE(7,2)|MASS CONCENTRATION(7,2)|EMISSION HUNDRED MILLION TON(7,1)|SILICEOUS INTIMA(7,1)|PH DETECTOR(6,4)|ALKALINE POLLUTION(6,1)|CULTURE ANAEROBIC BACTERIUM(6,1)|MOUNTAIN FIRE(6,1)|NATURAL DISASTER FREQUENT OCCURRENCE(6,1)|PARTICLE AGGLOMERATION(6,1)|STEEL SLAG SLURRY PH(6,1)|WET DECARBURIZATION(6,1)|CARBON FIXATION REACTION(5,6)|WET MILLING(5,6)|FREEZE DRYING(5,5)|ECOLOGICAL ENVIRONMENT(5,1)|ECONOMIC BENEFIT(5,1)|WASTE LYE(5,1)|AMMONIUM BICARBONATE SOLUTION(4,2)|GAS OUTLET(4,2)|REGULAR TIME(4,2)|CA DISSOLUTION(4,1)|CALCIUM CARBONATE PRECIPITATE(4,1)|CARBONIZATION(4,1)|FINE PARTICLE(4,1)|HORIZONTAL AGITATOR BALL MILL(4,1)|INDUSTRY SCALE(4,1)|OVERFLOW GAS PH(4,1)|PROMOTION(4,1)|QUENCHING TREATMENT(4,1)|RAW IRON(4,1)|SOLIDIFICATION REACTION(4,1)|STEEL REFINING(4,1)|STEEL SLAG RESIDUE SOLID(4,1)|STEEL SLAG WATER QUENCHING(4,1)|ALKALI SODIUM HYDROXIDE(3,1)| (CN115069362)|1. A method for carbon fixation and emission reduction of wet-milling steel slag in a steel plant is characterized by comprising the following steps:|(1) Quenching molten steel slag produced by a steel plant in a water quenching way, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with a median particle size of 20-500 mu m;|(2) The steel slag powder and water are mixed according to the mass ratio of 1: (1-4) mixing and stirring to obtain steel slag slurry;|(3) CO-containing effluent from steel plants 2 The flue gas is collected in a gas collecting bottle;|(4) Introducing 100 parts by mass of steel slag slurry and 5-18 parts by mass of flue gas into a horizontal stirred ball mill, adding grinding media and a stabilizer accounting for 1-5% of the mass of steel slag powder for wet grinding, and carrying out carbon fixation by utilizing the steel slag slurry;|(5) Drying the wet ground slurry to obtain CO 2 Solidifying the material;|the stabilizer adopts one or a combination of more of sucrose, sodium gluconate, sodium citrate and sodium metaphosphate; the grinding medium is used in an amount of 50-100 parts by mass.|2. The method for carbon sequestration and emission reduction of wet-milled steel slag in steel works according to claim 1, which is characterized in that:|CO in the flue gas 2 The mass concentration of (2) is 10-15%.|3. The method for carbon sequestration and emission reduction of wet-milled steel slag in steel works according to claim 1, which is characterized in that:|the grinding medium is zirconia balls and/or agate balls.|4. The method for carbon sequestration and emission reduction of wet-milled steel slag in steel works according to claim 1, which is characterized in that:|the grinding medium is prepared from grinding balls with the spherical diameters of 3-5 mm, grinding balls with the spherical diameters of 20-30 mm and grinding balls with the spherical diameters of 80-90 mm, wherein the mass ratio of the grinding balls with the spherical diameters of 3-5 mm, the grinding balls with the spherical diameters of 20-30 mm and the grinding balls with the spherical diameters of 80-90 mm is (1-3): 2: (3-1).|5. The method for carbon sequestration and emission reduction of wet-milled steel slag in steel works according to claim 1, which is characterized in that:|the step (4) is specifically as follows:|adding 100 parts by mass of steel slag slurry, a stabilizer accounting for 1-5% of the mass of steel slag powder and a grinding medium into a horizontal stirring ball mill, starting wet grinding and simultaneously introducing 5-18 parts by mass of flue gas; meanwhile, monitoring the pH value of overflowed gas of the horizontal stirring ball mill, and if the pH value of the overflowed gas is less than 7 when the fume is started to be introduced, reducing the fume introduction speed until the pH value of the overflowed gas reaches 7; and (3) detecting the pH value of the wet-grinding slurry at regular time in the wet-grinding process, and stopping wet-grinding when the pH value of the slurry is less than 7. (CN115069362)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of industrial solid waste treatment and environmental protection, and particularly relates to a method for carbon fixation and emission reduction of wet-grinding steel slag in a steel plant and application thereof.|BACKGROUND ART|[0002] Since the industrial revolution, energy consumption and CO have been expanding with the expansion of various industrial scales 2 Is increasingly dischargedMany. Since 1960 CO 2 The emissions of (2) have risen year by year, so far global CO 2 The annual emission of (2) reaches 322.8 hundred million tons, compared with the CO in 1960 2 The annual discharge amount is 90 hundred million tons, and the rise amplitude is up to 258.6 percent. And CO 2 The concentration level in the atmosphere also maintains a faster growth rate, and the CO in the atmosphere has been 1860 2 The concentration has increased from 288ppm to 411ppm, and the rise is as high as 42.7%. CO in greenhouse gases 2 The contribution ratio to the greenhouse effect is up to 50%, the accumulation of greenhouse gases in the atmosphere directly leads to the generation of the greenhouse effect, and the greenhouse effect leads to the frequent occurrence of natural disasters such as forest fires, floods, drought and the like.|[0003] Through the rapid development of the steel industry, china has become the largest steel production and consumption country in the world, and the steel yield accounts for about one fifth of the steel yield worldwide. The iron and steel industry brings great economic benefit and simultaneously generates a plurality of problems. On the one hand, a large amount of CO is generated during steelmaking 2 Emissions, about two tons of CO are produced per ton of crude iron produced 2 Emissions, 2019, global coarse steel yield of 19 hundred million tons, CO in the annual steel industry 2 About 38 hundred million tons of global artificial CO are discharged 2 7% of the emissions. On the other hand, steel slag is produced in the steelmaking process, the discharge amount of the steel slag is about 15% -20% of the steel yield, a large amount of steel slag occupies more and more land, the land is alkalized by the alkalinity of the steel slag, the ecological environment is polluted and destroyed, and a method is found to reasonably use the steel slag. Taking into account CO 2 The solidification reaction occurs in an alkaline environment, and a large amount of alkaline steel slag generated by a steel plant is used for CO 2 Has great potential and prospect in curing and sealing, but the prior method for fixing carbon by utilizing steel slag has the difficult problem which is partially difficult to solve.|[0004] In the chinese patent publication No. CN 102240501A, a method for carbon sequestration and emission reduction is disclosed, which includes: A. absorbing the discharged carbon dioxide by an absorption tower; B. calcining a carbon-fixing raw material and ammonium salt together, and reacting to generate ammonia gas and a salt solid product, wherein the carbon-fixing raw material contains metal elements capable of forming a precipitate with carbonate; C. introducing the produced ammonia gas into an absorption tower to react with carbon dioxide, and adding water to obtain an ammonium bicarbonate solution; D. b, placing the salt solid product obtained in the step B into water for leaching; E. and C, introducing the ammonium bicarbonate solution obtained in the step D into the liquid obtained by leaching in the step D to react to produce carbonate. The method has complex process, high cost caused by high-temperature calcination and waste gas and waste liquid generated in the carbon fixing process, and is not beneficial to environmental protection.|[0005] In the Chinese patent publication No. CN 104860474A, a method for fixing carbon and biologically treating sulfur-containing waste lye is disclosed, which uses biotechnology, needs to culture anaerobic bacteria special for fixing carbon, and needs to use strong alkali sodium hydroxide in a plurality of procedures, and has the advantages of complex process, difficult control, high cost and low carbon fixing rate.|[0006] In the Chinese patent publication No. CN 108246090A, a process method for wet decarburization by utilizing steel slag slurry is disclosed, and comprises the following steps: preparing the steel slag into steel slag slurry, wherein the steel slag slurry enters from the upper part of an absorption tower, and carbon dioxide-containing flue gas enters from the lower part of the absorption tower, and the steel slag slurry is fully contacted with the flue gas, so that decarburization is realized. However, the reaction efficiency and the carbon fixation rate of the method are low, and the method needs to be further improved.|[0007] In summary, the existing carbon fixing method generally has the problem that the carbon fixing rate and the cost are difficult to be compatible, and the waste gas and the waste liquid of most carbon fixing methods are not beneficial to environmental protection.|DISCLOSURE|Disclosure of Invention|[0008] The invention aims to provide a method for carbon sequestration and emission reduction of wet-milled steel slag in a steel plant and application thereof, wherein the method has obviously higher reaction efficiency and carbon sequestration rate.|[0009] The invention takes materials locally, utilizes a large amount of steel slag waste solids produced by the steel plant, and utilizes the steel slag to discharge CO containing gas discharged by the steel plant 2 The flue gas is used for carbon fixation, the cost is low, the reaction efficiency is high, the carbon fixation rate is high, the carbon emission of a steel plant can be obviously reduced, and the obtained steel slag carbon fixation product can be also used for concrete production.|[0010] The technical scheme of the invention is as follows:|[0011] a method for carbon fixation and emission reduction of wet-milling steel slag in a steel plant comprises the following steps:|[0012] (1) Quenching molten steel slag produced by a steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with the median particle size of 20-500 mu m;|[0013] (2) The steel slag powder and water are mixed according to the mass ratio of 1: (1-4) mixing and stirring to obtain steel slag slurry;|[0014] (3) CO-containing effluent from steel plants 2 The flue gas is collected in a gas collecting bottle;|[0015] (4) Introducing 100 parts by mass of steel slag slurry and 5-18 parts by mass of flue gas into a horizontal stirred ball mill, adding grinding media and a stabilizer accounting for 1-5% of the mass of steel slag powder for wet grinding, and carrying out carbon fixation by utilizing the steel slag slurry;|[0016] (5) Drying the wet ground slurry to obtain CO 2 And curing the material.|[0017] In some embodiments, CO in the flue gas 2 The mass concentration of (2) is 10-15%.|[0018] In some embodiments, the stabilizer is one or more of sucrose, sodium gluconate, sodium citrate, sodium metaphosphate.|[0019] In some embodiments, the milling media are zirconia balls and/or agate balls.|[0020] Further, the grinding medium is graded by grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm, wherein the mass ratio of the grinding balls with the ball diameter of 3-5 mm, the grinding balls with the ball diameter of 20-30 mm and the grinding balls with the ball diameter of 80-90 mm is (1-3): 2: (3-1).|[0021] In some embodiments, the grinding media is used in an amount of 50 to 10 parts by mass.|[0022] In some embodiments, the rotational speed of the horizontal stirred ball mill is set to 20-50 r/s.|[0023] In some embodiments, step (4) is specifically:|[0024] adding 100 parts by mass of steel slag slurry, a stabilizer accounting for 1-5% of the mass of steel slag powder and a grinding medium into a horizontal stirring ball mill, starting wet grinding and simultaneously introducing 5-18 parts by mass of flue gas; meanwhile, monitoring the pH value of overflowed gas of the horizontal stirring ball mill, and if the pH value of the overflowed gas is less than 7 when the fume is started to be introduced, reducing the fume introduction speed until the pH value of the overflowed gas reaches 7; and (3) detecting the pH value of the wet-grinding slurry at regular time in the wet-grinding process, and stopping wet-grinding when the pH value of the slurry is less than 7. Since the original steel slag slurry is alkaline, when the pH value of the original steel slag slurry is less than 7, the steel slag slurry and the flue gas are completely reacted.|[0025] In some embodiments, the pH value of the overflow gas is monitored by arranging a pH detector at the air outlet of the horizontal stirring ball mill.|[0026] The agglomeration phenomenon of steel slag particles easily occurs when steel slag is pulped, and the coated steel slag particles are difficult to contact CO 2 The method comprises the steps of carrying out a first treatment on the surface of the In the carbon fixation reaction process, calcium and magnesium ions in the steel slag particles can slowly dissolve out, and in the calcium and magnesium ion dissolution process, siliceous film structures can be generated in the steel slag particles to prevent the calcium and magnesium ions from continuously dissolving out. Dissolved calcium and magnesium ions and CO dissolved in water 2 The reaction forms a layer of compact carbonate film structure on the surface of the steel slag particles to prevent CO 2 And continuously contacting with the steel slag. And the produced calcium carbonate precipitate is precipitated towards the bottom of the ball mill, the newly generated carbonate covers the steel slag slurry, and more steel slag particles are wrapped and covered. The above reasons lead to low utilization rate, low reaction efficiency and low carbon fixation rate of the existing steel slag carbon fixation.|[0027] The invention solves the problems by utilizing wet grinding and steel slag carbon fixation. The molten steel slag is quenched and fixed by water when the internal crystal structure of the steel slag is not stable, and compared with the common air-cooled steel slag, the steel slag has higher activity. The wet grinding is carried out by utilizing the grinding medium to impact the particles in the steel slag slurry at a high speed under the drive of the stirring shaft so as to reduce the particle size of the particles.|[0028] The agglomerated particles can be further opened in the wet grinding process, so that the steel slag particles in the slurry are more uniformly dispersed. While introducing CO 2 Wet grinding is carried out at the same time in the solidification reaction stage, and the grinding medium not only can grind the grain diameter of the steel slag particles to be less than 20 mu m, but also can obviously increase the specific surface area of the steel slag; the coating lamellar structure outside the free calcium oxide and the free magnesium oxide can be destroyed, and the active ingredients are released; can also destroy siliceous inner membranes formed in the interior of steel slag particlesThe structure of the steel slag is that calcium and magnesium ions in the steel slag particles are further dissolved out.|[0029] In addition, the quenched steel slag can generate hydration reaction in the wet grinding process, and the generated calcium hydroxide is used for generating CO 2 Can play a certain promoting role, thereby greatly improving the carbon fixation rate of the steel slag slurry. And the grinding medium is hit during wet grinding to collide with the steel slag particles, and the process can lead the steel slag particles to collide with CO 2 The calcium carbonate carbonized film generated on the surface of the steel slag particles is broken during the reaction, and the dense carbonized film can expose fresh surface after being broken, thus the steel slag particles can continue to react with CO 2 Contact and reaction. The addition of the stabilizer can prevent the agglomeration of the steel slag during wet grinding, so that the steel slag particles are dispersed more uniformly in the solution, and the carbonization rate of the steel slag is improved.|[0030] The invention has the following characteristics and beneficial effects:|[0031] (1) The carbon fixation rate of the steel slag can be remarkably improved:|[0032] the wet grinding technology is utilized to refine the grain diameter of the steel slag, increase the specific surface area of the steel slag and facilitate the carbon fixation reaction; the siliceous inner membrane in the steel slag can be destroyed by wet grinding, and the continuous dissolution of calcium and magnesium ions is promoted; the addition of the stabilizer can prevent the agglomeration of the steel slag in the grinding process, so that the steel slag particles can be uniformly dispersed in the slurry; the grinding and carbon fixation reactions are carried out simultaneously, and the grinding medium continuously impacts the steel slag particles to break down compact carbonized layers on the surfaces of the steel slag particles and expose fresh surfaces and CO 2 Fully contacts, thereby greatly improving the utilization rate, the reaction efficiency and the carbon fixation rate of the steel slag.|[0033] (2) The cost can be obviously reduced:|[0034] the steel slag is waste solid in the steel plant, can be obtained locally in the steel plant, can obtain water-cooled slag in the process of refining steel, avoids energy consumption and transportation cost for heating the steel slag to a molten state in other application scenes, and can also avoid CO 2 Is not limited by the cost of transportation.|[0035] (3) The reaction environment is warmed;|[0036] the invention can realize high-efficiency CO without high-temperature and high-pressure environment assistance 2 Solidifying and sealing.|[0037] (4) Is favorable for environmental protection:|[0038] the flue gas and the steel slag discharged in the production process of the steel plant are utilized to carry out carbon fixation reaction, so that the waste in the steel plant is consumed in situ, the nature of the carbon fixation reaction is acid-base neutralization, and the alkalinity of the steel slag slurry is eliminated when the carbon fixation reaction is finally completed; in addition, in the carbon fixing process, not only calcium ions and magnesium ions play a role in carbon fixing, but also other metal ions in the steel slag slurry play a role in carbon fixing, so that the harm of heavy metals contained in the steel slag slurry is eliminated after the carbon fixing reaction is completed. When the solid carbon steel slag slurry is piled up and treated later, the alkaline pollution and heavy metal pollution of the steel slag to the environment can be avoided.|[0039] In summary, the method provided by the invention has the advantages of high carbon fixation rate, low cost and environmental friendliness, and is suitable for popularization and production.|INVENTION MODE|Detailed Description|[0040] The invention will be further explained with reference to examples. The examples are given for illustrative purposes only and are not intended to limit the scope of the present invention.|[0041] In the wet grinding process, steel slag slurry is discharged into a horizontal stirring ball mill, a gas collecting cylinder is connected with a gas inlet of the horizontal stirring ball mill through a gas inlet valve, and pH value at a gas overflow port of the horizontal stirring ball mill is monitored by pH detection equipment. The flow of the flue gas entering the horizontal stirring ball mill is regulated and controlled by adjusting an air inlet valve of the gas collecting bottle.|[0042] Example 1|[0043] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with the median particle size of 500 mu m; collecting the flue gas (CO in the flue gas) in the flue of a certain steel plant 2 About 10% of the mass content) in the gas collection bottle for standby; and (3) taking 100 parts by mass of steel slag powder and 100 parts by mass of water, fully mixing and stirring to obtain steel slag slurry. Pouring the steel slag slurry into a horizontal stirring ball mill, adding 1 part by mass of sodium gluconate and 50 parts by mass of grinding media (in the embodiment, the grinding media are compounded by grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the mass ratio of 1:2:1), and performing airtight horizontal stirring ball millingAnd a feed inlet of the machine. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detector at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 20r/s for wet grinding, and simultaneously introducing flue gas into the horizontal stirring ball mill at a flow rate of 5 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was not fully reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 10.5 using a pH measuring instrument.|[0044] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining mass loss of the sample at 500-900 ℃ which is CO generated after carbonate decomposition 2 The mass loss of the calculated sample at the temperature of 500-900 ℃ is 0.87g, so that the carbon fixation rate of the steel slag slurry in one hour is 8.7%.|[0045] Example 2|[0046] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with the median particle size of 100 mu m; collecting flue gas (CO) in a flue of a steel plant 2 About 10% of the content) is stored in a gas collecting bottle for standby; and (3) taking 100 parts by mass of steel slag powder and 100 parts by mass of water, fully mixing and stirring to obtain steel slag slurry. Pouring the steel slag slurry into a horizontal stirred ball mill, adding 1 part by mass of sodium gluconate and 50 parts by mass of grinding media (in the embodiment, the grinding media are compounded by grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the mass ratio of 1:2:1), and sealing a feed inlet of the horizontal stirred ball mill. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detection instrument at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 30r/s for wet grinding, and simultaneously introducing flue gas into the horizontal stirring ball mill at a flow rate of 9 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was not fully reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 9.3 using a pH tester.|[0047] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining the mass loss of the sample at 500-900 ℃ which is the product after carbonate decompositionRaw CO 2 The mass loss of the calculated sample at the temperature of 500-900 ℃ is 0.94g, so that the carbon fixation rate of the steel slag slurry in one hour is 9.4%.|[0048] Example 3|[0049] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with a median particle size of 20 mu m; collecting flue gas (CO) in a flue of a steel plant 2 About 10% of the content) is stored in a gas collecting bottle for standby; and (3) fully mixing and stirring 100 parts by mass of steel slag powder and 200 parts by mass of water to obtain steel slag slurry. Pouring the steel slag slurry into a horizontal stirred ball mill, adding 2 parts by mass of sodium gluconate and 50 parts by mass of grinding media (in the embodiment, the grinding media are prepared by mixing grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the mass ratio of 1:2:2), and sealing a feed inlet of the horizontal stirred ball mill. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detection instrument at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 40r/s for wet grinding, and simultaneously introducing smoke into the horizontal stirring ball mill at a flow rate of 12 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was not fully reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 8.1 using a pH tester.|[0050] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining mass loss of the sample at 500-900 ℃ which is CO generated after carbonate decomposition 2 The mass loss of the sample at the temperature of 500-900 ℃ is 1.12g, so the carbon fixation rate of the slurry in one hour is about 11.2%.|[0051] Example 4|[0052] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with a median particle size of 20 mu m; collecting flue gas (CO) in a flue of a steel plant 2 About 10% of the content) is stored in a gas collecting bottle for standby; and (3) fully mixing and stirring 100 parts by mass of steel slag powder and 300 parts by mass of water to obtain steel slag slurry. The steel slag slurry was poured into a horizontal stirred ball mill, and 3 parts by mass of sodium gluconate and 50 parts by mass of a grinding medium (this solidIn the embodiment, the grinding medium consists of grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the weight ratio of 1:1:1 mass ratio), and sealing the feed inlet of the horizontal stirred ball mill. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detection instrument at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 40r/s for wet grinding, and simultaneously introducing smoke into the horizontal stirring ball mill at a flow rate of 15 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was not fully reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 8.7 using a pH tester.|[0053] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining mass loss of the sample at 500-900 ℃ which is CO generated after carbonate decomposition 2 The mass loss of the calculated sample at the temperature of 500-900 ℃ is 1.02g, so that the carbon fixation rate of the steel slag slurry in one hour is 10.2%, and the slurry is not fully reacted.|[0054] Example 5|[0055] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with a median particle size of 20 mu m; collecting flue gas (CO) in a flue of a steel plant 2 About 10% of the content) is stored in a gas collecting bottle for standby; and (3) fully mixing and stirring 100 parts by mass of steel slag powder and 400 parts by mass of water to obtain steel slag slurry. Pouring the steel slag slurry into a horizontal stirring ball mill, adding 5 parts by mass of sodium gluconate to obtain the steel slag slurry and 100 parts by mass of grinding media (in the embodiment, the grinding media are compounded by grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the mass ratio of 3:2:3), and sealing a feed inlet of the horizontal stirring ball mill. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detection instrument at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 50r/s for wet grinding, and simultaneously introducing flue gas into the horizontal stirring ball mill at a flow rate of 18 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was completely reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 6.8 using a pH tester.|[0056] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining mass loss of the sample at 500-900 ℃ which is CO generated after carbonate decomposition 2 The mass loss of the calculated sample at the temperature of 500-900 ℃ is 1.25g, so the carbon fixation rate of the steel slag slurry in one hour is about 12.5%.|[0057] Comparative example|[0058] Collecting flue gas (CO) in a flue of a steel plant 2 The content is about 10%) is stored in a gas collecting bottle for standby, 100 parts by mass of steel slag powder with the median particle size of 100 mu m and 100 parts by mass of water are fully mixed and stirred to obtain steel slag slurry, 200 parts by mass of steel slag slurry is poured into a horizontal stirring ball mill, a feed inlet is sealed, then a gas inlet is connected with the gas collecting bottle, and a pH detecting instrument is arranged at a gas outlet. The pH of the slurry measured by a pH tester after one hour is 11.3, the sampled slurry is freeze-dried, ground and sieved, 10g of dried sample is obtained for thermogravimetric analysis and test, thermogravimetric analysis data are obtained for analysis, and the mass loss of the sample at 500-900 ℃ is the mass of carbon dioxide generated after the decomposition of carbonate, and the mass loss of the sample is 0.33g, so that the carbon fixation rate of the steel slag slurry in one hour is 3.3%.|[0059] The carbon fixation rate data of examples 1 to 5 and comparative example are shown in Table 1, and it is clear from Table 1 that the steel slag slurry of the present invention has significantly higher carbon fixation rate than the comparative example in which the steel slag slurry is directly used for carbon fixation, and can significantly improve the utilization rate of the steel slag slurry as a carbon fixation material, thereby greatly reducing CO in steel plants 2 Discharge amount.|[0060] Table 1 carbon fixation data for examples 1-5 and comparative examples|[0061] Numbering deviceRotational speedMedian particle diameter of steel slagSlurry pH after wet milling for 1hCarbon fixation rateExample 120r/min500μm9.78.7%Example 230r/min100μm9.39.4%Example 340r/min20μm8.111.2%Example 440r/min20μm8.710.2%Example 550r/min20μm6.812.5%Comparative example 10100μm11.93.3%|[0062] The foregoing is merely exemplary of the present invention to enable those skilled in the art to understand or practice the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. (CN115069362)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of industrial solid waste treatment and environmental protection, and particularly relates to a method for carbon fixation and emission reduction of wet-grinding steel slag in a steel plant and application thereof.|BACKGROUND ART|[0002] Since the industrial revolution, energy consumption and CO have been expanding with the expansion of various industrial scales 2 Is increasingly dischargedMany. Since 1960 CO 2 The emissions of (2) have risen year by year, so far global CO 2 The annual emission of (2) reaches 322.8 hundred million tons, compared with the CO in 1960 2 The annual discharge amount is 90 hundred million tons, and the rise amplitude is up to 258.6 percent. And CO 2 The concentration level in the atmosphere also maintains a faster growth rate, and the CO in the atmosphere has been 1860 2 The concentration has increased from 288ppm to 411ppm, and the rise is as high as 42.7%. CO in greenhouse gases 2 The contribution ratio to the greenhouse effect is up to 50%, the accumulation of greenhouse gases in the atmosphere directly leads to the generation of the greenhouse effect, and the greenhouse effect leads to the frequent occurrence of natural disasters such as forest fires, floods, drought and the like.|[0003] Through the rapid development of the steel industry, china has become the largest steel production and consumption country in the world, and the steel yield accounts for about one fifth of the steel yield worldwide. The iron and steel industry brings great economic benefit and simultaneously generates a plurality of problems. On the one hand, a large amount of CO is generated during steelmaking 2 Emissions, about two tons of CO are produced per ton of crude iron produced 2 Emissions, 2019, global coarse steel yield of 19 hundred million tons, CO in the annual steel industry 2 About 38 hundred million tons of global artificial CO are discharged 2 7% of the emissions. On the other hand, steel slag is produced in the steelmaking process, the discharge amount of the steel slag is about 15% -20% of the steel yield, a large amount of steel slag occupies more and more land, the land is alkalized by the alkalinity of the steel slag, the ecological environment is polluted and destroyed, and a method is found to reasonably use the steel slag. Taking into account CO 2 The solidification reaction occurs in an alkaline environment, and a large amount of alkaline steel slag generated by a steel plant is used for CO 2 Has great potential and prospect in curing and sealing, but the prior method for fixing carbon by utilizing steel slag has the difficult problem which is partially difficult to solve.|[0004] In the chinese patent publication No. CN 102240501A, a method for carbon sequestration and emission reduction is disclosed, which includes: A. absorbing the discharged carbon dioxide by an absorption tower; B. calcining a carbon-fixing raw material and ammonium salt together, and reacting to generate ammonia gas and a salt solid product, wherein the carbon-fixing raw material contains metal elements capable of forming a precipitate with carbonate; C. introducing the produced ammonia gas into an absorption tower to react with carbon dioxide, and adding water to obtain an ammonium bicarbonate solution; D. b, placing the salt solid product obtained in the step B into water for leaching; E. and C, introducing the ammonium bicarbonate solution obtained in the step D into the liquid obtained by leaching in the step D to react to produce carbonate. The method has complex process, high cost caused by high-temperature calcination and waste gas and waste liquid generated in the carbon fixing process, and is not beneficial to environmental protection.|[0005] In the Chinese patent publication No. CN 104860474A, a method for fixing carbon and biologically treating sulfur-containing waste lye is disclosed, which uses biotechnology, needs to culture anaerobic bacteria special for fixing carbon, and needs to use strong alkali sodium hydroxide in a plurality of procedures, and has the advantages of complex process, difficult control, high cost and low carbon fixing rate.|[0006] In the Chinese patent publication No. CN 108246090A, a process method for wet decarburization by utilizing steel slag slurry is disclosed, and comprises the following steps: preparing the steel slag into steel slag slurry, wherein the steel slag slurry enters from the upper part of an absorption tower, and carbon dioxide-containing flue gas enters from the lower part of the absorption tower, and the steel slag slurry is fully contacted with the flue gas, so that decarburization is realized. However, the reaction efficiency and the carbon fixation rate of the method are low, and the method needs to be further improved.|[0007] In summary, the existing carbon fixing method generally has the problem that the carbon fixing rate and the cost are difficult to be compatible, and the waste gas and the waste liquid of most carbon fixing methods are not beneficial to environmental protection.|DISCLOSURE|Disclosure of Invention|[0008] The invention aims to provide a method for carbon sequestration and emission reduction of wet-milled steel slag in a steel plant and application thereof, wherein the method has obviously higher reaction efficiency and carbon sequestration rate.|[0009] The invention takes materials locally, utilizes a large amount of steel slag waste solids produced by the steel plant, and utilizes the steel slag to discharge CO containing gas discharged by the steel plant 2 The flue gas is used for carbon fixation, the cost is low, the reaction efficiency is high, the carbon fixation rate is high, the carbon emission of a steel plant can be obviously reduced, and the obtained steel slag carbon fixation product can be also used for concrete production.|[0010] The technical scheme of the invention is as follows:|[0011] a method for carbon fixation and emission reduction of wet-milling steel slag in a steel plant comprises the following steps:|[0012] (1) Quenching molten steel slag produced by a steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with the median particle size of 20-500 mu m;|[0013] (2) The steel slag powder and water are mixed according to the mass ratio of 1: (1-4) mixing and stirring to obtain steel slag slurry;|[0014] (3) CO-containing effluent from steel plants 2 The flue gas is collected in a gas collecting bottle;|[0015] (4) Introducing 100 parts by mass of steel slag slurry and 5-18 parts by mass of flue gas into a horizontal stirred ball mill, adding grinding media and a stabilizer accounting for 1-5% of the mass of steel slag powder for wet grinding, and carrying out carbon fixation by utilizing the steel slag slurry;|[0016] (5) Drying the wet ground slurry to obtain CO 2 And curing the material.|[0017] In some embodiments, CO in the flue gas 2 The mass concentration of (2) is 10-15%.|[0018] In some embodiments, the stabilizer is one or more of sucrose, sodium gluconate, sodium citrate, sodium metaphosphate.|[0019] In some embodiments, the milling media are zirconia balls and/or agate balls.|[0020] Further, the grinding medium is graded by grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm, wherein the mass ratio of the grinding balls with the ball diameter of 3-5 mm, the grinding balls with the ball diameter of 20-30 mm and the grinding balls with the ball diameter of 80-90 mm is (1-3): 2: (3-1).|[0021] In some embodiments, the grinding media is used in an amount of 50 to 10 parts by mass.|[0022] In some embodiments, the rotational speed of the horizontal stirred ball mill is set to 20-50 r/s.|[0023] In some embodiments, step (4) is specifically:|[0024] adding 100 parts by mass of steel slag slurry, a stabilizer accounting for 1-5% of the mass of steel slag powder and a grinding medium into a horizontal stirring ball mill, starting wet grinding and simultaneously introducing 5-18 parts by mass of flue gas; meanwhile, monitoring the pH value of overflowed gas of the horizontal stirring ball mill, and if the pH value of the overflowed gas is less than 7 when the fume is started to be introduced, reducing the fume introduction speed until the pH value of the overflowed gas reaches 7; and (3) detecting the pH value of the wet-grinding slurry at regular time in the wet-grinding process, and stopping wet-grinding when the pH value of the slurry is less than 7. Since the original steel slag slurry is alkaline, when the pH value of the original steel slag slurry is less than 7, the steel slag slurry and the flue gas are completely reacted.|[0025] In some embodiments, the pH value of the overflow gas is monitored by arranging a pH detector at the air outlet of the horizontal stirring ball mill.|[0026] The agglomeration phenomenon of steel slag particles easily occurs when steel slag is pulped, and the coated steel slag particles are difficult to contact CO 2 The method comprises the steps of carrying out a first treatment on the surface of the In the carbon fixation reaction process, calcium and magnesium ions in the steel slag particles can slowly dissolve out, and in the calcium and magnesium ion dissolution process, siliceous film structures can be generated in the steel slag particles to prevent the calcium and magnesium ions from continuously dissolving out. Dissolved calcium and magnesium ions and CO dissolved in water 2 The reaction forms a layer of compact carbonate film structure on the surface of the steel slag particles to prevent CO 2 And continuously contacting with the steel slag. And the produced calcium carbonate precipitate is precipitated towards the bottom of the ball mill, the newly generated carbonate covers the steel slag slurry, and more steel slag particles are wrapped and covered. The above reasons lead to low utilization rate, low reaction efficiency and low carbon fixation rate of the existing steel slag carbon fixation.|[0027] The invention solves the problems by utilizing wet grinding and steel slag carbon fixation. The molten steel slag is quenched and fixed by water when the internal crystal structure of the steel slag is not stable, and compared with the common air-cooled steel slag, the steel slag has higher activity. The wet grinding is carried out by utilizing the grinding medium to impact the particles in the steel slag slurry at a high speed under the drive of the stirring shaft so as to reduce the particle size of the particles.|[0028] The agglomerated particles can be further opened in the wet grinding process, so that the steel slag particles in the slurry are more uniformly dispersed. While introducing CO 2 Wet grinding is carried out at the same time in the solidification reaction stage, and the grinding medium not only can grind the grain diameter of the steel slag particles to be less than 20 mu m, but also can obviously increase the specific surface area of the steel slag; the coating lamellar structure outside the free calcium oxide and the free magnesium oxide can be destroyed, and the active ingredients are released; can also destroy siliceous inner membranes formed in the interior of steel slag particlesThe structure of the steel slag is that calcium and magnesium ions in the steel slag particles are further dissolved out.|[0029] In addition, the quenched steel slag can generate hydration reaction in the wet grinding process, and the generated calcium hydroxide is used for generating CO 2 Can play a certain promoting role, thereby greatly improving the carbon fixation rate of the steel slag slurry. And the grinding medium is hit during wet grinding to collide with the steel slag particles, and the process can lead the steel slag particles to collide with CO 2 The calcium carbonate carbonized film generated on the surface of the steel slag particles is broken during the reaction, and the dense carbonized film can expose fresh surface after being broken, thus the steel slag particles can continue to react with CO 2 Contact and reaction. The addition of the stabilizer can prevent the agglomeration of the steel slag during wet grinding, so that the steel slag particles are dispersed more uniformly in the solution, and the carbonization rate of the steel slag is improved.|[0030] The invention has the following characteristics and beneficial effects:|[0031] (1) The carbon fixation rate of the steel slag can be remarkably improved:|[0032] the wet grinding technology is utilized to refine the grain diameter of the steel slag, increase the specific surface area of the steel slag and facilitate the carbon fixation reaction; the siliceous inner membrane in the steel slag can be destroyed by wet grinding, and the continuous dissolution of calcium and magnesium ions is promoted; the addition of the stabilizer can prevent the agglomeration of the steel slag in the grinding process, so that the steel slag particles can be uniformly dispersed in the slurry; the grinding and carbon fixation reactions are carried out simultaneously, and the grinding medium continuously impacts the steel slag particles to break down compact carbonized layers on the surfaces of the steel slag particles and expose fresh surfaces and CO 2 Fully contacts, thereby greatly improving the utilization rate, the reaction efficiency and the carbon fixation rate of the steel slag.|[0033] (2) The cost can be obviously reduced:|[0034] the steel slag is waste solid in the steel plant, can be obtained locally in the steel plant, can obtain water-cooled slag in the process of refining steel, avoids energy consumption and transportation cost for heating the steel slag to a molten state in other application scenes, and can also avoid CO 2 Is not limited by the cost of transportation.|[0035] (3) The reaction environment is warmed;|[0036] the invention can realize high-efficiency CO without high-temperature and high-pressure environment assistance 2 Solidifying and sealing.|[0037] (4) Is favorable for environmental protection:|[0038] the flue gas and the steel slag discharged in the production process of the steel plant are utilized to carry out carbon fixation reaction, so that the waste in the steel plant is consumed in situ, the nature of the carbon fixation reaction is acid-base neutralization, and the alkalinity of the steel slag slurry is eliminated when the carbon fixation reaction is finally completed; in addition, in the carbon fixing process, not only calcium ions and magnesium ions play a role in carbon fixing, but also other metal ions in the steel slag slurry play a role in carbon fixing, so that the harm of heavy metals contained in the steel slag slurry is eliminated after the carbon fixing reaction is completed. When the solid carbon steel slag slurry is piled up and treated later, the alkaline pollution and heavy metal pollution of the steel slag to the environment can be avoided.|[0039] In summary, the method provided by the invention has the advantages of high carbon fixation rate, low cost and environmental friendliness, and is suitable for popularization and production.|INVENTION MODE|Detailed Description|[0040] The invention will be further explained with reference to examples. The examples are given for illustrative purposes only and are not intended to limit the scope of the present invention.|[0041] In the wet grinding process, steel slag slurry is discharged into a horizontal stirring ball mill, a gas collecting cylinder is connected with a gas inlet of the horizontal stirring ball mill through a gas inlet valve, and pH value at a gas overflow port of the horizontal stirring ball mill is monitored by pH detection equipment. The flow of the flue gas entering the horizontal stirring ball mill is regulated and controlled by adjusting an air inlet valve of the gas collecting bottle.|[0042] Example 1|[0043] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with the median particle size of 500 mu m; collecting the flue gas (CO in the flue gas) in the flue of a certain steel plant 2 About 10% of the mass content) in the gas collection bottle for standby; and (3) taking 100 parts by mass of steel slag powder and 100 parts by mass of water, fully mixing and stirring to obtain steel slag slurry. Pouring the steel slag slurry into a horizontal stirring ball mill, adding 1 part by mass of sodium gluconate and 50 parts by mass of grinding media (in the embodiment, the grinding media are compounded by grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the mass ratio of 1:2:1), and performing airtight horizontal stirring ball millingAnd a feed inlet of the machine. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detector at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 20r/s for wet grinding, and simultaneously introducing flue gas into the horizontal stirring ball mill at a flow rate of 5 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was not fully reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 10.5 using a pH measuring instrument.|[0044] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining mass loss of the sample at 500-900 ℃ which is CO generated after carbonate decomposition 2 The mass loss of the calculated sample at the temperature of 500-900 ℃ is 0.87g, so that the carbon fixation rate of the steel slag slurry in one hour is 8.7%.|[0045] Example 2|[0046] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with the median particle size of 100 mu m; collecting flue gas (CO) in a flue of a steel plant 2 About 10% of the content) is stored in a gas collecting bottle for standby; and (3) taking 100 parts by mass of steel slag powder and 100 parts by mass of water, fully mixing and stirring to obtain steel slag slurry. Pouring the steel slag slurry into a horizontal stirred ball mill, adding 1 part by mass of sodium gluconate and 50 parts by mass of grinding media (in the embodiment, the grinding media are compounded by grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the mass ratio of 1:2:1), and sealing a feed inlet of the horizontal stirred ball mill. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detection instrument at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 30r/s for wet grinding, and simultaneously introducing flue gas into the horizontal stirring ball mill at a flow rate of 9 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was not fully reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 9.3 using a pH tester.|[0047] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining the mass loss of the sample at 500-900 ℃ which is the product after carbonate decompositionRaw CO 2 The mass loss of the calculated sample at the temperature of 500-900 ℃ is 0.94g, so that the carbon fixation rate of the steel slag slurry in one hour is 9.4%.|[0048] Example 3|[0049] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with a median particle size of 20 mu m; collecting flue gas (CO) in a flue of a steel plant 2 About 10% of the content) is stored in a gas collecting bottle for standby; and (3) fully mixing and stirring 100 parts by mass of steel slag powder and 200 parts by mass of water to obtain steel slag slurry. Pouring the steel slag slurry into a horizontal stirred ball mill, adding 2 parts by mass of sodium gluconate and 50 parts by mass of grinding media (in the embodiment, the grinding media are prepared by mixing grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the mass ratio of 1:2:2), and sealing a feed inlet of the horizontal stirred ball mill. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detection instrument at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 40r/s for wet grinding, and simultaneously introducing smoke into the horizontal stirring ball mill at a flow rate of 12 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was not fully reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 8.1 using a pH tester.|[0050] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining mass loss of the sample at 500-900 ℃ which is CO generated after carbonate decomposition 2 The mass loss of the sample at the temperature of 500-900 ℃ is 1.12g, so the carbon fixation rate of the slurry in one hour is about 11.2%.|[0051] Example 4|[0052] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with a median particle size of 20 mu m; collecting flue gas (CO) in a flue of a steel plant 2 About 10% of the content) is stored in a gas collecting bottle for standby; and (3) fully mixing and stirring 100 parts by mass of steel slag powder and 300 parts by mass of water to obtain steel slag slurry. The steel slag slurry was poured into a horizontal stirred ball mill, and 3 parts by mass of sodium gluconate and 50 parts by mass of a grinding medium (this solidIn the embodiment, the grinding medium consists of grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the weight ratio of 1:1:1 mass ratio), and sealing the feed inlet of the horizontal stirred ball mill. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detection instrument at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 40r/s for wet grinding, and simultaneously introducing smoke into the horizontal stirring ball mill at a flow rate of 15 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was not fully reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 8.7 using a pH tester.|[0053] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining mass loss of the sample at 500-900 ℃ which is CO generated after carbonate decomposition 2 The mass loss of the calculated sample at the temperature of 500-900 ℃ is 1.02g, so that the carbon fixation rate of the steel slag slurry in one hour is 10.2%, and the slurry is not fully reacted.|[0054] Example 5|[0055] Quenching molten steel slag produced by a certain steel plant by water quenching, and then crushing, deironing and dry grinding in sequence to obtain steel slag powder with a median particle size of 20 mu m; collecting flue gas (CO) in a flue of a steel plant 2 About 10% of the content) is stored in a gas collecting bottle for standby; and (3) fully mixing and stirring 100 parts by mass of steel slag powder and 400 parts by mass of water to obtain steel slag slurry. Pouring the steel slag slurry into a horizontal stirring ball mill, adding 5 parts by mass of sodium gluconate to obtain the steel slag slurry and 100 parts by mass of grinding media (in the embodiment, the grinding media are compounded by grinding balls with the ball diameter of 3-5 mm, grinding balls with the ball diameter of 20-30 mm and grinding balls with the ball diameter of 80-90 mm according to the mass ratio of 3:2:3), and sealing a feed inlet of the horizontal stirring ball mill. And then connecting an air inlet of the horizontal stirring ball mill with an air collecting bottle, arranging a pH detection instrument at an air outlet, starting the horizontal stirring ball mill at a rotating speed of 50r/s for wet grinding, and simultaneously introducing flue gas into the horizontal stirring ball mill at a flow rate of 18 parts by mass/h. After one hour, wet milling and aeration were stopped, at which time the slurry was completely reacted, and the pH of the slurry in the horizontal stirred ball mill was measured to be 6.8 using a pH tester.|[0056] Freeze drying the sampled slurry, grinding and sieving, taking 10g of dried sample for thermogravimetric analysis and test, obtaining thermogravimetric analysis data for analysis, and obtaining mass loss of the sample at 500-900 ℃ which is CO generated after carbonate decomposition 2 The mass loss of the calculated sample at the temperature of 500-900 ℃ is 1.25g, so the carbon fixation rate of the steel slag slurry in one hour is about 12.5%.|[0057] Comparative example|[0058] Collecting flue gas (CO) in a flue of a steel plant 2 The content is about 10%) is stored in a gas collecting bottle for standby, 100 parts by mass of steel slag powder with the median particle size of 100 mu m and 100 parts by mass of water are fully mixed and stirred to obtain steel slag slurry, 200 parts by mass of steel slag slurry is poured into a horizontal stirring ball mill, a feed inlet is sealed, then a gas inlet is connected with the gas collecting bottle, and a pH detecting instrument is arranged at a gas outlet. The pH of the slurry measured by a pH tester after one hour is 11.3, the sampled slurry is freeze-dried, ground and sieved, 10g of dried sample is obtained for thermogravimetric analysis and test, thermogravimetric analysis data are obtained for analysis, and the mass loss of the sample at 500-900 ℃ is the mass of carbon dioxide generated after the decomposition of carbonate, and the mass loss of the sample is 0.33g, so that the carbon fixation rate of the steel slag slurry in one hour is 3.3%.|[0059] The carbon fixation rate data of examples 1 to 5 and comparative example are shown in Table 1, and it is clear from Table 1 that the steel slag slurry of the present invention has significantly higher carbon fixation rate than the comparative example in which the steel slag slurry is directly used for carbon fixation, and can significantly improve the utilization rate of the steel slag slurry as a carbon fixation material, thereby greatly reducing CO in steel plants 2 Discharge amount.|[0060] Table 1 carbon fixation data for examples 1-5 and comparative examples|[0061] Numbering deviceRotational speedMedian particle diameter of steel slagSlurry pH after wet milling for 1hCarbon fixation rateExample 120r/min500μm9.78.7%Example 230r/min100μm9.39.4%Example 340r/min20μm8.111.2%Example 440r/min20μm8.710.2%Example 550r/min20μm6.812.5%Comparative example 10100μm11.93.3%|[0062] The foregoing is merely exemplary of the present invention to enable those skilled in the art to understand or practice the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. Family Number|(101844296)|101844296|Abstract|(CN115069362B B)|The invention discloses a steel plant wet grinding steel slag carbon sequestration and emission reduction method , which comprises : ( 1 ) carrying out water quenching and quenching on molten steel slag produced by a steel plant , and sequentially carrying out crushing , iron removal and dry grinding to obtain steel slag powder with a median particle size of 20-500 [ mu ] m ; ( 2 ) mixing the steel slag powder and water according to a mass ratio of 1 : ( 1-4 ) , and stirring to obtain steel slag slurry ; ( 3 ) collecting CO2 - containing flue gas discharged by the steel plant into a gas collection bottle ; ( 4 ) introducing 100 parts by mass of the steel slag slurry and 5-18 parts by mass of flue gas into a horizontal stirring ball mill , adding a grinding medium and a stabilizer accounting for 1-5% of the mass of the steel slag powder for wet grinding , and fixing carbon by using the steel slag slurry ; and ( 5 ) drying the wet - ground slurry to obtain the CO2 curing material . The method has the advantages of high carbon sequestration rate , low cost and environmental protection , and is suitable for popularization and production . |CPC codes|(CN115069362B B)|B01D - 053/62 |B01D - 053/82 |IPC codes|(CN115069362B B)|B01D - 053/62 |B01D - 053/82 |Title|(CN115069362 A)|Method for carbon sequestration and emission reduction of wet - ground steel slag of iron and steel plant and application | Chemical engineering|Environmental technology B01D-053/62|B01D-053/82|B02C-017/10|B02C-023/00|B02C-023/06|B02C-2201/06 B01D-053/62|B01D-053/82|B02C-017/10|B02C-023/00|B02C-023/06|B02C-2201/06 B01D-053/62|B01D-053/82|B02C-017/10|B02C-023/00|B02C-023/06 B01D-053/62|B01D-053/82|B02C-017/10|B02C-023/00|B02C-023/06 CN116396053|CN115872650|CN119040529|WO202525814|CN116274270|CN116969710B|CN116832605B|CN116283141B|CN116332559B CN116396053 105666122 WHO=Examiner SELF=Y CAT=Y|CN115872650 104375980 WHO=Examiner SELF=N CAT=Y|CN119040529 112403288 WHO=Examiner SELF=N CAT=A|WO202525814 107157345 WHO=Examiner SELF=Y CAT=A|CN116274270 105465920 WHO=Examiner SELF=Y CAT=A|CN116969710B 107057189 WHO=Examiner SELF=Y|CN116832605B 106744235 WHO=Examiner SELF=Y|CN116283141B 105422195 WHO=Examiner SELF=Y|CN116332559B 105513068 WHO=Examiner SELF=Y JP06184610|CN113718070|CN113634114|CN112691535|CN108246090|CN108779505|CN108883984|JP2017214262|CN106145720|JP6184610|CN103111186|US20130287672|CN102671519|CN102534068|CN101898087|CN102240501|CN101851071|CN101475999|JP2008120607|KR20060023206|CN1557970|US4272498 JP06184610 28440447 WHO=Examiner SELF=N CAT=A|CN113718070 97333311 WHO=Examiner SELF=N|CN113634114 96986576 WHO=Examiner SELF=N|CN112691535 93746009 WHO=Examiner SELF=Y|CN108246090 80496801 WHO=Examiner SELF=N|CN108779505 80682022 WHO=Examiner SELF=N|CN108883984 80763030 WHO=Examiner SELF=N|JP2017214262 77993560 WHO=Examiner SELF=N|CN106145720 74666064 WHO=Examiner SELF=N|JP6184610 80778106 WHO=Examiner SELF=N|CN103111186 73658034 WHO=Examiner SELF=N|US20130287672 45466114 WHO=Examiner SELF=N|CN102671519 7857479 WHO=Examiner SELF=N|CN102534068 7738770 WHO=Examiner SELF=N|CN101898087 7160498 WHO=Examiner SELF=N|CN102240501 7453319 WHO=Examiner SELF=N|CN101851071 7094502 WHO=Examiner SELF=N|CN101475999 6774280 WHO=Examiner SELF=N|JP2008120607 32754379 WHO=Examiner SELF=N|KR20060023206 34954205 WHO=Examiner SELF=N|CN1557970 61967400 WHO=Examiner SELF=N|US4272498 42440644 WHO=Examiner SELF=N 2008120607|H06184610|2017214262 JP06184610; CN102534068; JP2008120607; JP6184610; CN103111186; CN108246090; CN108779505; CN108883984; US4272498; CN102240501; CN101851071; JP2017214262; CN101475999; CN101898087; CN102671519; CN106145720; CN112691535; CN113634114; CN113718070; CN1557970; KR20060023206; US20130287672 GRANTED (CN115069362)|GRANTED ALIVE (CN115069362)|ALIVE (CN115069362)|LEGAL DETAILS FOR CN115069362|Actual or expected expiration date=2042-05-30|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-05-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210599827|Application date=2022-05-30|Standardized application number=2022CN-0599827|Event publication date=2022-09-20|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115069362|Publication stage code=A|Publication date=2022-09-20|Standardized publication number=CN115069362|Event publication date=2022-09-20|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-10-11|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-11-21|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN115069362|Publication stage code=B|Publication date=2023-11-21|Standardized publication number=CN115069362B|Event publication date=2023-11-21|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN115069362)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRgwpqVUI8k9Bj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=VbfF8losmKykusW5YnwiFrmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN115069362)|CN|(CN115069362)|CN (CN115069362)|NAME=HUBEI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN|(CN115069362)|NAME=HUBEI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN115069362)|NAME=WANG DONGDONG;WUHAN SINOPOWER PATENT AGENCY , REG=42237|(CN115069362)|NAME=WANG DONGDONG;WUHAN SINOPOWER PATENT AGENCY , REG=42237 (CN115069362)|NAME=SU YING|NAME=LI CHENGHAO|NAME=HE XINGYANG|NAME=ZHENG ZHENGQI|NAME=YANG JIN|NAME=WANG YINGBIN|NAME=TAN HONGBO|(CN115069362)|NAME=SU YING|NAME=LI CHENGHAO|NAME=HE XINGYANG|NAME=ZHENG ZHENGQI|NAME=YANG JIN|NAME=WANG YINGBIN|NAME=TAN HONGBO 0 1 Titre: (CN115069362)|Method for carbon fixation and emission reduction of wet-milling steel slag in steel plant and application of method Résumé: (CN115069362)|The invention discloses a steel plant wet grinding steel slag carbon sequestration and emission reduction method, which comprises: (1) carrying out water quenching and quenching on molten steel slag produced by a steel plant, and sequentially carrying out crushing, iron removal and dry grinding to obtain steel slag powder with a median particle size of 20-500 [mu] m; (2) mixing the steel slag powder and water according to a mass ratio of 1: (1-4), and stirring to obtain steel slag slurry; (3) collecting CO2-containing flue gas discharged by the steel plant into a gas collection bottle; (4) introducing 100 parts by mass of the steel slag slurry and 5-18 parts by mass of flue gas into a horizontal stirring ball mill, adding a grinding medium and a stabilizer accounting for 1-5% of the mass of the steel slag powder for wet grinding, and fixing carbon by using the steel slag slurry; and (5) drying the wet-ground slurry to obtain the CO2 curing material. The method has the advantages of high carbon sequestration rate, low cost and environmental protection, and is suitable for popularization and production. 30 Abstract gpt-4o-mini no The method focuses on carbon sequestration using steel slag and flue gas, which does not align with the accelerated weathering of silicate or alkaline minerals for CO₂ capture.
33 CN202211169882 CN202211169882 CN115430401|CN115430401 102897237 CN115430401 B 2023-06-23 [CN115430401B]|CN115430401 A 2022-12-06 [CN115430401] 2022-09-23 2022-09-23 2023-06-23|2022-12-06 (CN115430401B)|2023-06-23 (CN115430401)|2042-09-23 (CN115430401)|Sulfur-doped biochar with carbon fixation and pollution reduction effects as well as preparation method and application thereof (CN115430401)|The invention relates to sulfur-doped biochar with both carbon sequestration and pollution reduction effects as well as a preparation method and application thereof, and belongs to the technical field of biochar. The preparation method of the sulfur-doped biochar with both carbon sequestration and pollution reduction effects comprises the following steps: crushing, grinding and air-drying a biomass raw material, sieving to obtain a powdery biochar precursor, mixing the powdery biochar precursor with a sulfur-containing sodium salt, adding water for dissolving, stirring at a constant speed, fully dipping, and heating in a muffle furnace to obtain the sulfur-doped biochar. The sulfur-doped biochar material is low in price, simple to prepare and good in stability, and compared with original biochar, the sulfur-doped biochar not only has a carbon sequestration effect, but also has a remarkable remediation effect on Cr-polluted soil. SUN YAT SEN UNIVERSITY (CN115430401)|SUN YAT-SEN UNIVERSITY ([CN])|(CN115430401)|SUN YAT-SEN UNIVERSITY ([CN]) ZHAO NAN|LUO QIAN|YANG ZAIKUAN|LIU KUNYUAN|XU QIANTING|ZHANG WEIHUA|CHOU RONGLIANG (CN115430401)|ZHAO NAN|LUO QIAN|YANG ZAIKUAN|LIU KUNYUAN|XU QIANTING|ZHANG WEIHUA|CHOU RONGLIANG|(CN115430401)|ZHAO NAN|LUO QIAN|YANG ZAIKUAN|LIU KUNYUAN|XU QIANTING|ZHANG WEIHUA|CHOU RONGLIANG (CN115430401)|CHEN JING;SCIHEAD IP LAW FIRM|Reg. Nb: 44202 (CN115430401)|Cr (VI) is easy to migrate in soil and pore water, even spread into surface water or underground water, and is absorbed by animals and plants and generates toxic action, even the Cr (VI) is enriched into human bodies through drinking water or food chains, so that serious threat is formed to human health, and nausea, diarrhea, liver and kidney injury, dermatitis, internal bleeding and respiratory system problems can be caused under acute contact.|The preparation method provided by the invention has the advantages of high efficiency, low cost, high efficiency, stability, economy, environmental protection, high energy recovery and easiness in application, and the sulfur-doped biochar with strong adsorption capacity to Cr (VI) can be prepared at a lower temperature (300-700 ℃), so that energy consumption can be effectively reduced.|The traditional soil chromium pollution restoration technology such as electrodynamic force, leaching, chemical reduction and the like has the defects of high energy consumption, high cost and secondary pollution, and the bioremediation has the limitations of long restoration period, difficult bacteria screening and the like, so that the technology is difficult to be applied to engineering practice.| (CN115430401)|1. The application of the sulfur-doped biochar in repairing Cr (VI) pollution is characterized in that the preparation raw materials of the sulfur-doped biochar comprise biomass raw materials and sodium salt containing sulfur, and the mass ratio of the biomass raw materials to the sodium salt containing sulfur is 1: (1-4);the preparation method of the sulfur-doped biochar comprises the following steps:s1, mixing powdered biochar raw materials with sulfur-containing sodium salt, adding water for dissolution, stirring at a constant speed, fully soaking, and drying to obtain a premix;s2, heating the premix in the step S1 to 300-700 ℃ at a heating rate of 10 ℃/min under the anoxic condition, maintaining for 1-3h, and cooling to obtain the sulfur-doped biochar;the sulfur-containing sodium salt is Na 2 S 2 O 3 ;The specific surface area of the sulfur-doped biochar is 100-120 m 2 Per gram, the total pore volume is 0.05-0.1 cm 3 Per g, mesoporous volume > 0.04cm 3 Per gram, micropore volume of 0.01-0.05 cm 3 /g, wherein the average pore diameter is 2-4 nm;the biomass raw material comprises at least one of straw, dicranopteris pedata, miscanthus and rice husk.| (CN115430401)|In a second aspect, the invention provides a method for preparing the sulfur-doped biochar, comprising the following steps:|The invention relates to sulfur-doped biochar with carbon fixation and pollution reduction effects, and a preparation method and application thereof, and belongs to the technical field of biochar.|in a first aspect, the invention provides sulfur-doped biochar, wherein the preparation raw materials of the sulfur-doped biochar comprise biomass raw materials and sodium salt containing sulfur, and the mass ratio of the biomass raw materials to the sodium salt containing sulfur is 1: (1-4);| (CN115430401)|SULFUR DOPED BIOCHAR(100,65)|CARBON FIXATION(100,7)|CONTAMINATION(100,7)|POLLUTION REDUCTION(100,5)|REPAIRING CR(100,5)|POWDERY BIOCHAR PRECURSOR(82,2)|SOIL CHROMIUM POLLUTION RESTORATION(80,1)|SOIL CHROMIUM POLLUTION(55,1)|DICRANOPTERIS PEDATA(46,4)|KIDNEY INJURY(38,1)|DIFFICULT BACTERIUM SCREENING(36,1)|BIOMASS FEEDSTOCK(33,1)|SULFUR(29,16)|MICROPORE VOLUME(27,2)|ELECTRODYNAMIC FORCE(27,1)|BIOREMEDIATION(26,1)|MESOPORE VOLUME(25,3)|BIOCHAR(24,28)|SODIUM SALT(24,16)|PREMIX(24,7)|ADSORPTION CAPACITY(24,3)|CR POLLUTED SOIL(24,2)|THREAT(24,1)|BIOMASS RAW MATERIAL(23,13)|DERMATITIS(22,1)|DISSOLUTION(21,6)|ANOXIC CONDITION(21,5)|DIARRHEA(20,1)|GRAM(19,4)|MISCANTHUS(19,3)|DICRANOPTERIS PEDATA NONIMPREGNATED POWDER(19,2)|RICE HUSK(19,2)|STRAW(18,4)|MEDIAN PORE DIAMETER(18,3)|SULFUR DOPED BIOCHAR DIAMETER(18,2)|NAUSEA(18,1)|SOAKING(17,8)|LEACHING(17,2)|ECONOMY(17,1)|DRY POLLUTED SOIL(16,3)|LIVER(16,1)|TOTAL PORE VOLUME(15,3)|SOAKED MISCANTHUS POWDER PREMIX(15,2)|ACUTE CONTACT(15,1)|ANIMAL(15,1)|ENVIRONMENTAL PROTECTION(15,1)|PRICE(15,1)|GROUND(14,32)|SOIL REPAIRING CR POLLUTION(14,2)|CONSTANT SPEED(13,8)|CLEANED SULFUR DOPED BIOCHAR(13,4)|PREPARATION RAW MATERIAL(13,2)|HUMAN HEALTH(13,1)|MUFFLE FURNACE(12,7)|DICRANOPTERIS PEDATA POWDER PREMIX(12,1)|FOOD CHAIN(12,1)|LONG RESTORATION PERIOD LIMITATION(12,1)|PREMIXED DICRANOPTERIS PEDATA POWDER(12,1)|SOIL CR POLLUTION REMEDIATION(11,2)|DRINKING WATER(11,1)|UNDERGROUND WATER(11,1)|HEATING RATE(10,6)|MASS RATIO(10,6)|SULFUR DOPING(10,5)|CARBON FIXING(10,1)|LONG RESTORATION PERIOD(10,1)|TOXIC ACTION(10,1)|SULFUR DOPED BIOCHAR MATERIAL(9,9)|GRINDING(9,5)|ELECTRON SCANNING MICROSCOPE(9,3)|PORE WATER(9,1)|SOAKED STRAW POWDER PREMIX(9,1)|ENERGY CONSUMPTION(8,2)|CHEMICAL REDUCTION(8,1)|CR CONTAMINATION REMEDIATION(8,1)|CR MORPHOLOGICAL TRANSFORMATION(8,1)|CR MORPHOLOGY EXTRACTION EXPERIMENT(8,1)|IMMERSED STRAW POWDER PREMIX(8,1)|POLLUTED REPAIR SOIL(8,1)|SULFUR DOPED BIOCHAR ACIDITY(8,1)|BIOCHAR RAW MATERIAL(7,6)|BIOCHAR MATRIX(7,2)|BIOCHAR PH(7,2)|SULFUR INCORPORATION(7,2)|BIOCHAR ACCOUNT MESOPOROUS VOLUME(7,1)|BIOCHAR ASH(7,1)|CR POLLUTION REPAIRING REDUCTION(7,1)|HIGH ENERGY CONSUMPTION DEFECT(7,1)|HUMAN BODY(7,1)|RESPIRATORY SYSTEM(7,1)|SOIL CONTAMINATION(7,1)|IMPURITY(6,5)|CR MORPHOLOGICAL CHANGE(6,2)|SUCCESSFULLY INTRODUCED SULFUR(6,2)|CALCIUM ACID SULFURTHE PRECIPITATION(6,1)|DOC DISSOLUTION(6,1)|RADIX PULVERIZATION(6,1)|SOIL CULTURE EXPERIMENT(6,1)|AROMATICITY(5,3)|CHROMIUM CONTAMINATION(5,1)|CRUSHED STRAW(5,1)|ENVIRONMENTALLY FRIENDLY CR(5,1)|HIGH ENERGY CONSUMPTION(5,1)|HIGH ENERGY RECOVERY(5,1)|MISCANTHUS SINENSIS POWDER(5,1)|MORPHOLOGICAL EXTRACTION(5,1)|PAID ATTENTION(5,1)|PARAMOUNT IMPORTANCE(5,1)|SOIL REMEDIATION EXPERIMENT(5,1)|SOIL TOC CONTENT(5,1)|SULFUR DOPED BIOCHAR CONTENT(5,1)|TOXIC POLLUTANT(5,1)|SULFUR DOPED BIOCHAR SURFACE(4,5)|CRUSHING(4,3)|STRUCTURAL CHANGE(4,3)|ASH CONTENT(4,2)|BIOMASS PYROLYSIS(4,2)|ADSORPTION DESORPTION CURVE(4,1)|BIOCHAR COMPARISON(4,1)|CR CONTAMINATED SOIL(4,1)|ELECTRON GRAVITY(4,1)|INDUSTRIAL ACTIVITY SITE GROUNDWATER(4,1)|O1S PEAK(4,1)|RAW BIOCHAR(4,1)|RE CR(4,1)|RESTORED SOIL(4,1)|SOLID WASTE LEACHING TOXICITY(4,1)|SULFUR DOPED BIOCHAR DECREASE(4,1)|XPS SPECTRUM(4,1)|MAGNETIC STIRRER(3,4)|SOIL SAMPLE(3,4)|BAKING OVEN(3,3)|POWDERED BIOCHAR RAW MATERIAL(3,3)|SBC(3,3)|ATOMIC PERCENTAGE CONTENT(3,2)|MAXIMUM FIXATION(3,2)|RETORT(3,2)|TOPOGRAPHY(3,2)|CARBONIZATION TEMPERATURE(3,1)|CARBONYL CARBON(3,1)|CARBOXYL CARBON(3,1)|DOC CONTENT(3,1)|DRIED SOIL(3,1)|HYDROPHILICITY(3,1)|IRON POT(3,1)|IRON TANK(3,1)|REDUCING CR MOBILITY(3,1)|REMOVING CONTAMINATION(3,1)|SEALED ACTIVATING MEDIUM(3,1)|SODIUM SALT IMPREGNATION(3,1)|SULFATE RADICAL(3,1)|SULFUR GENERATION(3,1)||(CN115430401)|SULFUR DOPED BIOCHAR(100,64)|THEREFORE SULFUR DOPED BIOCHAR(100,8)|POLLUTION REDUCTION FUNCTION(100,4)|CARBON FIXATION(100,2)|DISSOLVE POWDERY BIOCHAR PRECURSOR(77,1)|SOIL CHROMIUM POLLUTION REMEDIATION(67,1)|SOIL CR CONTAMINATION REMEDIATION(58,1)|BIOMASS FEEDSTOCK(55,2)|SCREENING BACTERIA(48,1)|REPAIRING CR POLLUTION(46,5)|CONTAMINATION RISK(44,1)|REPAIRING CR CONTAMINATION(44,1)|SULFUR(43,22)|KIDNEY INJURY(42,1)|SOIL CHROMIUM(40,1)|PASSIVE PLANT(37,1)|PREMIX(36,8)|CR POLLUTED SOIL(33,1)|ELECTRODYNAMIC FORCE(31,1)|ANOXIC CONDITION(30,6)|BIOREMEDIATION(29,1)|RECOVERING ENERGY(28,1)|BIOCHAR(27,31)|SODIUM SALT(27,17)|SOAKING(27,5)|THREAT(27,1)|ADSORPTION CAPACITY(25,3)|RESTORATION(25,1)|DERMATITIS(24,1)|BIOMASS RAW MATERIAL(23,11)|DIARRHEA(22,1)|SODIUM SULFUR(22,1)|NAUSEA(20,1)|CARBON FIXING(19,4)|DICRANOPTERIS PEDATA POWDER PREMIX(19,2)|MICROPORE VOLUME(19,2)|ECONOMY(19,1)|MOLTEN SALT MEDIUM(19,1)|POWDERED BIOCHAR RAW MATERIAL(18,6)|POLLUTION REMEDIATION(18,5)|DRY CONTAMINATED SOIL(18,2)|LIVER(18,1)|LONG REMEDIATION PERIOD(18,1)|LONG REMEDIATION PERIOD LIMITATION(18,1)|GROUND(17,26)|CONSTANT SPEED(17,8)|LEACHING(17,3)|MESOPORE VOLUME(17,3)|ACUTE CONTACT(17,1)|ENVIRONMENTAL PROTECTION(17,1)|GREEN LOW TOXICITY ADDITIVE(16,1)|HUMAN HEALTH(15,1)|RICE HULL(15,1)|BIOCHAR MATERIAL(14,12)|MUFFLE FURNACE(14,7)|CLEANED SULFUR DOPED BIOCHAR(14,4)|SOIL CR POLLUTION REMEDIATION(14,3)|CONTAMINATED REMEDIATION SOIL(14,2)|SOAKED STRAW POWDER PREMIX(14,2)|INTERNAL HEMORRHAGE(14,1)|PRICE(14,1)|CRUSHING(13,3)|MEDIAN PORE DIAMETER(13,2)|FOOD CHAIN(13,1)|HEATING RATE(12,5)|MASS RATIO(12,5)|DRINKING WATER(12,1)|SOAKED MISCANTHUS POWDER PREMIX(12,1)|UNDERGROUND WATER(12,1)|SULFUR DOPED BIOCHAR MATERIAL(11,10)|BIOCHAR RAW MATERIAL(11,7)|SULFUR DOPING(11,5)|REPAIRING SOIL CR POLLUTION(11,1)|TOXIC ACTION(11,1)|IRON TANK(10,6)|GRINDING(10,4)|ELECTRON SCANNING MICROSCOPE(10,3)|TOTAL PORE VOLUME(10,3)|LEACHING TOXICITY CRITERION(10,1)|MISCANTHUS SINENSIS POWDER PREMIX(10,1)|PORE WATER(10,1)|SOIL MORPHOLOGICAL TRANSFORMATION(10,1)|ENERGY CONSUMPTION(9,2)|BIOCHAR AROMATICITY(9,1)|CHEMICAL REDUCTION(9,1)|CR MORPHOLOGY EXTRACTION EXPERIMENT(9,1)|CR POLLUTION REPAIRING(9,1)|SULFUR DOPED BIOCHAR ACIDITY(9,1)|UNIMPREGNATED DICRANOPTERIS(9,1)|BIOCHAR MATRIX(8,2)|SOIL REMEDIATION EXPERIMENT(8,2)|BIOCHAR ACCOUNT MESOPOROUS VOLUME(8,1)|HEAVY METAL(8,1)|HIGH ENERGY CONSUMPTION DEFECT(8,1)|HUMAN BODY(8,1)|PYROLYZING BIOMASS(8,1)|RESPIRATORY SYSTEM(8,1)|RAW MATERIAL(7,3)|CR MORPHOLOGICAL CHANGE(7,2)|XPS SPECTRUM(7,2)|BIOCHAR ASH CONTENT(7,1)|BIOMASS PYROLYSIS(7,1)|CHROMIUM CONTAMINATION(7,1)|MICROPORE PORE(7,1)|REPAIRINGCR CONTAMINATED SOIL(7,1)|SOIL CULTURE EXPERIMENT(7,1)|IMPURITY(6,5)|CR MIGRATION(6,1)|ENVIRONMENTALLY FRIENDLY CR(6,1)|HIGH ENERGY CONSUMPTION(6,1)|MAGNETIC STIRRERSTIRRING(6,1)|MORPHOLOGICAL EXTRACTION(6,1)|O1S PEAK ATOMIC PERCENTAGE(6,1)|PRIORITY POLLUTANT(6,1)|SOIL DISSOLUTION(6,1)|STABILIZING ROLE(6,1)|TOXIC POLLUTANT(6,1)|TOPOGRAPHY(5,3)|VIRGIN(5,3)|BIOCHAR COMPARISON(5,1)|BIOCHAR CONTENT(5,1)|BIOCHAR PH(5,1)|CR TOXICITY(5,1)|ELECTRON GRAVITY(5,1)|INDUSTRIAL ACTIVITY SITE GROUNDWATER(5,1)|POWDER DISSOLUTION(5,1)|RAW BIOCHAR(5,1)|REPAIRING CR(5,1)|SOIL ACID LEACHING(5,1)|SOILTHE(5,1)|SOIL SAMPLE(4,4)|SULFUR DOPED BIOCHAR SURFACE(4,4)|MIXING SODIUM(4,2)|STRUCTURAL CHANGE(4,2)|ARTIFICIAL CLIMATE CHAMBER(4,1)|CALCIUM SULFATE PRECIPITATE(4,1)|CARBONYL CARBON(4,1)|CARBOXYL CARBON(4,1)|DOC CONTENT(4,1)|DRY LAND(4,1)|DRY POLLUTED SOIL(4,1)|DRYING OVEN(4,1)|ELEMENTAL COMPOSITION ANALYSIS(4,1)|EQUIVALENT SUBSTITUTION(4,1)|HYDROPHILICITY(4,1)|MIGRATION REDUCTION(4,1)|PREMIXTURE(4,1)|REMOVING CONTAMINATION(4,1)|SEAL ACTIVATION MEDIUM(4,1)|SULFUR DOPED BIOCHAR DIAMETER(4,1)|SULFUR GENERATION(4,1)|TREATING CR(4,1)|CARBON MONOXIDE(3,4)|CARBON SEQUESTRATION(3,3)|SBC(3,3)|ACID NEUTRAL(3,1)|ACIDIC GROUP(3,1)| (CN115430401)|1. The application of the sulfur-doped biochar in repairing Cr (VI) pollution is characterized in that the preparation raw materials of the sulfur-doped biochar comprise biomass raw materials and sodium salt containing sulfur, and the mass ratio of the biomass raw materials to the sodium salt containing sulfur is 1: (1-4);|the preparation method of the sulfur-doped biochar comprises the following steps:|s1, mixing powdered biochar raw materials with sulfur-containing sodium salt, adding water for dissolution, stirring at a constant speed, fully soaking, and drying to obtain a premix;|s2, heating the premix in the step S1 to 300-700 ℃ at a heating rate of 10 ℃/min under the anoxic condition, maintaining for 1-3h, and cooling to obtain the sulfur-doped biochar;|the sulfur-containing sodium salt is Na 2 S 2 O 3 ;|The specific surface area of the sulfur-doped biochar is 100-120 m 2 Per gram, the total pore volume is 0.05-0.1 cm 3 Per g, mesoporous volume > 0.04cm 3 Per gram, micropore volume of 0.01-0.05 cm 3 /g, wherein the average pore diameter is 2-4 nm;|the biomass raw material comprises at least one of straw, dicranopteris pedata, miscanthus and rice husk.|2. Use of sulfur-doped biochar according to claim 1 for repairing Cr (VI) pollution, wherein the mass ratio of biomass feedstock to sulfur-containing sodium salt is 1:3.|3. the use of sulfur-doped biochar according to claim 1 for repairing Cr (VI) pollution, wherein the diameter of the sulfur-doped biochar is less than or equal to 0.15mm.|4. Use of the sulfur-doped biochar according to claim 1 for repairing Cr (VI) pollution, wherein the sulfur-doped biochar is used for repairing Cr pollution in soil.|5. The use of sulfur-doped biochar for repairing Cr (VI) pollution according to claim 4, wherein the mass percentage of the sulfur-doped biochar in dry polluted soil is 1.5% -3.5%. (CN115430401)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of biochar, and relates to sulfur-doped biochar with carbon fixation and pollution reduction effects, and a preparation method and application thereof.|BACKGROUND ART|[0002] Cr exists in the soil mainly in the form of Cr (III) and Cr (VI), where Cr (VI) is one of the most toxic pollutants in soil and water systems, is a class a carcinogen with high toxicity, mutability and teratogenicity, and is listed by the us environmental protection agency as one of the preferred pollutants in soil and water environments. In the environment, cr (VI) mainly originates from artificial activities, and a large amount of Cr (VI) is released to the environment due to wide application in chemical industries such as electroplating, tanning, pigment, corrosion prevention, metal smelting, steel manufacturing and the like, and particularly serious chromium pollution exists in soil and groundwater of industrial activity sites related to chromates. Cr (VI) is easy to migrate in soil and pore water, even spread into surface water or underground water, and is absorbed by animals and plants and generates toxic action, even the Cr (VI) is enriched into human bodies through drinking water or food chains, so that serious threat is formed to human health, and nausea, diarrhea, liver and kidney injury, dermatitis, internal bleeding and respiratory system problems can be caused under acute contact. Thus, reduction of Cr (VI) to Cr (III), reducing Cr mobility, bioavailability and toxicity is currently the primary effective method of restoring Cr (VI) soil.|[0003] The traditional soil chromium pollution restoration technology such as electrodynamic force, leaching, chemical reduction and the like has the defects of high energy consumption, high cost and secondary pollution, and the bioremediation has the limitations of long restoration period, difficult bacteria screening and the like, so that the technology is difficult to be applied to engineering practice. Development of simple, efficient, economical and environmentally friendly Cr (VI) pollution removal technology is of paramount importance. Biochar is a simple and effective soil heavy metal stabilizer, and is widely paid attention to because of the advantages of low cost, wide raw material sources, higher efficiency, less pollution and the like. Biochar is a stable carbon material generated by pyrolysis of biomass under the anoxic condition, has the characteristics of large specific surface area, high porosity, multiple surface functional groups and the like, can provide a large number of active sites, has considerable adsorption capacity, has proved that the biochar has the capacity of providing electrons, has the effect of reducing toxicity by adsorption and reduction on Cr (VI), and has potential in repairing Cr-polluted soil. Biochar also has carbon storage capacity and can reduce or inhibit CO in soil 2 Is arranged in the air. The application of the biochar can increase the content of organic carbon in the soil and generate excitation effect with the organic matters in the soil.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to overcome the defects of the prior art and provide a preparation method and application of sulfur-doped biochar with carbon fixation and pollution reduction effects.|[0005] In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:|[0006] in a first aspect, the invention provides sulfur-doped biochar, wherein the preparation raw materials of the sulfur-doped biochar comprise biomass raw materials and sodium salt containing sulfur, and the mass ratio of the biomass raw materials to the sodium salt containing sulfur is 1: (1-4);|[0007] the preparation method of the sulfur-doped biochar comprises the following steps:|[0008] s1, mixing powdered biochar raw materials with sulfur-containing sodium salt, adding water for dissolution, stirring at a constant speed, fully soaking, and drying to obtain a premix;|[0009] s2, heating the premix in the step S1 to 300-700 ℃ at a heating rate of 10 ℃/min under the anoxic condition, maintaining for 1-3h, and cooling to obtain the sulfur-doped biochar.|[0010] The powdered biochar raw material in the step S1 can be directly the powdered biochar raw material existing in the prior art, or can be self-made, and the self-made method comprises the steps of but not limited to crushing, grinding and air-drying biomass raw materials, and then sieving the biomass raw materials with a 20-mesh sieve to obtain the powdered biochar raw material; the stirring mode and the stirring time depend on the biomass raw material, for example, the biomass raw material can be stirred on a magnetic stirrer at a constant speed for 12 hours after being dissolved by adding water; drying means and drying time include, but are not limited to, placing in an oven and baking at 105 ℃ for 48 hours.|[0011] The heating mode under the anoxic condition in the step S2 includes, but is not limited to, placing the premix into a can, sealing the can, and then placing the can into a muffle furnace for heating.|[0012] The method for cleaning and removing impurities of the sulfur-doped biochar comprises the steps of, but is not limited to, cleaning the sulfur-doped biochar by high-purity water, and washing off impurities on the surface of the biochar until the conductivity of filtrate is less than or equal to 18uS/cm. Finally, the cleaned sulfur-doped biochar is dried, ground and sieved (such as a 100-mesh sieve) and then stored for later use.|[0013] The sulfur-doped biochar prepared by the method has larger specific surface area and lower functional group content. Sulfur-doped biochar with successfully introduced sulfur-containing groups (-SO) 3 H. C= S, C-S) and the oxygen-containing functional groups are increased in content, the polarity is enhanced, while biochar produced directly from biomass pyrolysis tends to contain less sulfur-containing functional groups.|[0014] As a preferred embodiment of the sulfur-doped biochar of the present invention, the mass ratio of the biomass raw material to the sulfur-containing sodium salt is 1:3.|[0015] in the invention, the too low or too high content of the sodium salt in the sulfur-containing biomass material can cause the remarkable reduction of the Cr pollution repairing effect of the prepared sulfur-doped biochar material, and the applicant discovers that the mass ratio of the biomass raw material to the sodium salt in the sulfur-containing biomass material is 1: and 3, the prepared sulfur-doped biochar material has the best effect of repairing Cr pollution.|[0016] As a preferred embodiment of the sulfur-doped biochar, the biomass raw material comprises at least one of straw, dicranopteris pedata, miscanthus and rice husk.|[0017] As a preferred embodiment of the sulfur-doped biochar of the present invention, the sulfur-containing sodium salt is Na 2 S 2 O 3 。|[0018] Molten salt method is a common strategy for preparing biochar by adopting inert salt as a sealed activating medium. The biochar prepared by the molten salt method is widely applied to the fields of environmental treatment, gas adsorption, energy storage devices and the like. The invention adopts Na as a green low-toxicity additive in molten salt medium 2 S 2 O 3 To produce S-enriched biochar, thereby effectively adsorbing heavy metals, na from soil 2 S 2 O 3 Not only is environment-friendly, but also compared with other sodium salt containing sulfur, na 2 S 2 O 3 The prepared sulfur-doped biochar material has the best effect of repairing Cr pollution.|[0019] As a preferred embodiment of the sulfur-doped biochar, the diameter of the sulfur-doped biochar is less than or equal to 0.15mm.|[0020] As a preferred embodiment of the sulfur-doped biochar of the present invention, the specific surface area of the sulfur-doped biochar is 100 to 120m 2 Per gram, the total pore volume is 0.05-0.1 cm 3 Per g, mesoporous volume > 0.04cm 3 Per gram, micropore volume of 0.01-0.05 cm 3 And/g, the average pore diameter is 2-4 nm.|[0021] In a second aspect, the invention provides a method for preparing the sulfur-doped biochar, comprising the following steps:|[0022] s1, mixing powdered biochar raw materials with sulfur-containing sodium salt, adding water for dissolution, stirring at a constant speed, fully soaking, and drying to obtain a premix;|[0023] s2, heating the premix in the step S1 to 300-700 ℃ under the anoxic condition, maintaining for 1-3h, and cooling to obtain the sulfur-doped biochar.|[0024] The preparation method provided by the invention has the advantages of high efficiency, low cost, high efficiency, stability, economy, environmental protection, high energy recovery and easiness in application, and the sulfur-doped biochar with strong adsorption capacity to Cr (VI) can be prepared at a lower temperature (300-700 ℃), so that energy consumption can be effectively reduced.|[0025] In a third aspect, the invention provides the use of the sulfur-doped biochar in the remediation of Cr contamination.|[0026] As a preferred embodiment of the application of the sulfur-doped biochar in repairing Cr pollution, the sulfur-doped biochar is applied in repairing Cr pollution of soil.|[0027] The application of the sulfur-doped biochar in repairing Cr pollution of soil comprises the following steps:|[0028] and uniformly mixing the dry polluted soil with the sulfur-doped biochar, culturing for 7-21 days, and sampling to obtain the polluted and restored soil.|[0029] The sulfur-doped biochar prepared by the method can effectively repair the Cr pollution of the soil, reduce the pH value of alkaline soil, and has good development potential in the field of repairing the Cr pollution of the soil.|[0030] As a preferred implementation mode of the application of the sulfur-doped biochar in repairing Cr pollution, the mass percentage of the sulfur-doped biochar in dry polluted soil is 1.5% -3.5%.|[0031] Compared with the prior art, the invention has the beneficial effects that:|[0032] 1. the sulfur-doped biochar prepared by the method has larger specific surface area and lower functional group content. Sulfur-doped biochar with successfully introduced sulfur-containing groups (-SO) 3 H. C= S, C-S) and the content of oxygen-containing functional groups is increased and the polarity is enhanced.|[0033] 2. The sulfur-doped biochar is prepared at a lower temperature, namely 300-700 ℃, so that the energy consumption is effectively reduced.|[0034] 3. The sulfur-doped biochar prepared by the sulfur-containing sodium salt impregnation method has strong adsorption capacity on Cr (VI).|[0035] 4. The sulfur-doped biochar prepared by the method can effectively repair Cr-polluted soil and reduce the pH value of alkaline soil.|[0036] 5. The sulfur-doped biochar prepared by the method can reduce the concentration of soluble organic carbon content (DOC) in soilIncreasing total carbon content (TC) and total organic carbon content (TOC) of soil, and reducing CO in soil 2 The C content and the fertility of the soil are improved at the same time of the discharge of the water-soluble carbon dioxide, and a certain carbon fixation and emission reduction effect is achieved.|[0037] 6. The sulfur-doped biochar prepared by the method can be used as a repair material with high efficiency, low cost and environmental friendliness, and has good development potential in the field of Cr pollution repair.|DRAWINGS DESCRIPTION|[0038] FIG. 1 is an electron scanning microscope (SEM) morphology diagram and an EDS-Mapping diagram of the sulfur-doped biochar material prepared by the method.|[0039] FIG. 2 shows adsorption-desorption curves (a) and pore size distribution diagrams (b) of sulfur-doped biochar materials prepared by the method.|[0040] FIG. 3 is an XPS spectrum of the sulfur-doped biochar material prepared by the invention.|[0041] Fig. 4 is a graph showing the variation of DOC, TC and TOC in soil after soil remediation experiments using the sulfur-doped biochar material SBC600 and the original biochar BC600 prepared by the present invention.|[0042] Fig. 5 is a graph showing the change of the acid leaching concentration of (a) total Cr and (b) Cr (VI) in soil after a soil remediation experiment is performed by using the sulfur-doped biochar material SBC600 and the original biochar BC600 prepared by the method.|[0043] FIG. 6 is a graph showing the effect of different amounts of added sulfur-doped biochar material SBC600 and original biochar BC600 on the morphological change of Cr in soil.|[0044] FIG. 7 is a graph showing the effect of SBC600 and BC600 of sulfur-doped biochar material prepared by the invention on the morphological change of Cr in soil under different culture times.|[0045] FIG. 8 is a graph showing the variation of Cr (VI) content in soil after repairing Cr-contaminated soil by using the sulfur-doped biochar material SBC600 and the original biochar BC600 prepared by the method.|INVENTION MODE|Detailed Description|[0046] For a better description of the objects, technical solutions and advantages of the present invention, the present invention will be further described with reference to the following specific examples.|[0047] Example 1|[0048] The preparation method of the sulfur-doped biochar comprises the following steps:|[0049] (1) Pulverizing radix Osmundae, grinding, air drying, and sieving with 20 mesh sieve to obtain radix Osmundae powder.|[0050] (2) Na is mixed with 2 S 2 O 3 Mixing with the dicranopteris pedata powder according to the ratio of 3:1, adding water for dissolution, stirring for 12 hours at a constant speed on a magnetic stirrer, fully soaking, and then placing into a baking oven for baking at 105 ℃ for 48 hours until drying, thus obtaining the pre-mixed dicranopteris pedata powder after soaking.|[0051] (3) And (3) placing the immersed dicranopteris pedata powder premix into an iron tank to be sealed and placed into a muffle furnace, and heating to 600 ℃ at a heating rate of 10 ℃/min for 1h to obtain the high-temperature sulfur-doped biochar (SBC 600).|[0052] (4) And taking out the sulfur-doped biochar after the sulfur-doped biochar is naturally cooled, and cleaning the sulfur-doped biochar by using high-purity water to remove impurities on the surface of the sulfur-doped biochar until the conductivity of filtrate is less than or equal to 18uS/cm. Finally, the cleaned sulfur-doped biochar is dried, ground and sieved by a 100-mesh sieve for later use.|[0053] The electron scanning microscope (SEM) topography and EDS-Mapping of SBC600 were tested by conventional means in the art, and the results are shown in fig. 1, by which it was possible to observe that the S element was uniformly dispersed on the surface of SBC600, strongly demonstrating that S was doped into the biochar matrix.|[0054] Example 2|[0055] Example 2 differs from example 1 in that the sulfur-doped biochar (SBC 400) was heated to 400℃at a heating rate of 10℃per minute for 1 hour, i.e., a low temperature.|[0056] Example 3|[0057] The preparation method of the sulfur-doped biochar comprises the following steps:|[0058] (1) And (3) crushing, grinding and air-drying the straw, and sieving the crushed straw with a 20-mesh sieve to obtain straw powder.|[0059] (2) Na is mixed with 2 S 2 O 3 Mixing the powder with straw powder according to the ratio of 1:1, adding water for dissolution, stirring on a magnetic stirrer at a constant speed for 12 hours, fully soaking, and then putting into a baking oven for baking at 105 ℃ for 48 hours until the straw powder is dried, thus obtaining the soaked straw powder premix.|[0060] (3) And (3) placing the immersed straw powder premix into a steel pot, sealing and loading into a muffle furnace, and heating to 700 ℃ at a heating rate of 10 ℃/min for 3 hours to obtain the high-temperature sulfur-doped biochar (SBC 700).|[0061] (4) And taking out the sulfur-doped biochar after the sulfur-doped biochar is naturally cooled, and cleaning the sulfur-doped biochar by using high-purity water to remove impurities on the surface of the sulfur-doped biochar until the conductivity of filtrate is less than or equal to 18uS/cm. Finally, the cleaned sulfur-doped biochar is dried, ground and sieved by a 100-mesh sieve for later use.|[0062] Example 4|[0063] The preparation method of the sulfur-doped biochar comprises the following steps:|[0064] (1) Crushing, grinding and air-drying the miscanthus sinensis, and sieving with a 20-mesh sieve to obtain miscanthus sinensis powder.|[0065] (2) Na is mixed with 2 S 2 O 3 Mixing with the miscanthus powder according to the ratio of 4:1, adding water, dissolving, stirring on a magnetic stirrer at a constant speed for 12h, fully soaking, and then placing into a baking oven to bake at 105 ℃ for 48h until drying to obtain the soaked miscanthus powder premix.|[0066] (3) And (3) placing the soaked miscanthus powder premix into an iron pot, sealing and loading into a muffle furnace, and heating to 300 ℃ at a heating rate of 10 ℃/min for 1h to obtain the low-temperature sulfur-doped biochar (SBC 300).|[0067] (4) And taking out the sulfur-doped biochar after the sulfur-doped biochar is naturally cooled, and cleaning the sulfur-doped biochar by using high-purity water to remove impurities on the surface of the sulfur-doped biochar until the conductivity of filtrate is less than or equal to 18uS/cm. Finally, the cleaned sulfur-doped biochar is dried, ground and sieved by a 100-mesh sieve for later use.|[0068] The electron scanning microscope (SEM) topography and EDS-Mapping of examples 2-4 were similar to example 1, demonstrating that S was doped into the biochar matrix.|[0069] Example 5|[0070] An embodiment of the application of sulfur-doped biochar in Cr pollution in the invention, the application of sulfur-doped biochar in soil Cr pollution remediation in the embodiment comprises the following steps:|[0071] 40g of polluted soil is weighed, SBC600 with mass fractions of 1.5%, 2.5% and 3.5% is respectively added, 4 parallel treatments are arranged for each treatment, the dried soil and the SBC600 are uniformly mixed, then the mixture is cultivated in a climatic chamber, the constant temperature is set to 20.0 ℃, the relative humidity is set to 65%, and the samples are respectively taken on days 7, 14 and 21 to obtain the polluted repair soil. Soil moisture needs to be maintained at 60% of the field capacity of the soil during cultivation.|[0072] Example 6|[0073] An embodiment of the performance comparison of the sulfur-doped biochar and the original biochar comprises the comparison of biochar to N 2 Adsorption-desorption, pore size distribution, specific surface area, elemental composition, pH, type of carbon-containing groups and comparison of ratios.|[0074] In this example, examples 1 to 2 were used as experimental groups, comparative examples 1 to 2 were used as control groups, and comparative examples 1 to 2 were respectively:|[0075] comparative example 1|[0076] Comparative example 1 was different from example 1 in that the non-impregnated powder of dicranopteris pedata was placed in a retort and sealed in a muffle furnace to prepare high-temperature raw biochar (BC 600).|[0077] Comparative example 2|[0078] Comparative example 2 was different from example 2 in that the non-impregnated powder of dicranopteris pedata was placed in a retort and sealed in a muffle furnace to prepare a low-temperature raw biochar (BC 400).|[0079] FIG. 2 shows the pair N of sulfur-doped biochar of examples 1-2 and the original biochar of comparative examples 1-2 2 The adsorption-desorption curve of SBC600 is IV type, and H4 hysteresis appears under relatively high pressure, which indicates that the biochar is mesoporous biochar, the mesoporous volume of the biochar accounts for 66.2% of the total pore volume, and the average pore diameter is 2.51nm.|[0080] Table 1 shows BET specific surface areas of sulfur-doped biochars of examples 1 to 2 and original biochars of comparative examples 1 to 2.|[0081] TABLE 1|[0082] |[0083] As can be seen from Table 1, the specific surface area of SBC400 is 114m 2 Specific surface area of SBC600 is 109m 2 Per g, the increase of the specific surface area at low temperature after sulfur incorporation is probably due to the generation of sulfur-containing gas (H) at 300℃to 400 ℃ 2 S、SO 2 、CS 2 Etc.), thereby forming more pore structures. The specific surface area is probably reduced at high temperature because the salt is added to block the micropores, and the decomposition of the salt at high temperature and the functional group formed by the reaction on the surface of the biochar destroy the micropore structure, so that more reactive sites are provided for the surface of the biochar.|[0084] Table 2 shows elemental composition analysis and pH values of sulfur-doped biochar of examples 1 to 2 and the original biochar of comparative examples 1 to 2. The modified SBC600 had a sulfur content increased to 19.8%, again demonstrating successful sulfur incorporation. Compared with the original biochar, after sulfur doping, the contents of C, H and N elements and the pH value are reduced, the ash content, the ratio of O/C to (O+N)/C are increased, and the effects that the oxygen-containing functional group content of the sulfur-doped biochar is increased, the hydrophilicity and the polarity are enhanced, and the S atoms have higher electron gravity and can increase the surface polarity of the biochar are shown. The pH of the biochar is an indicator of the number of surface acidity or basic functional groups, and the acidity of sulfur-doped biochar may be caused by the generation of more acidic groups on the surface of the biochar during pyrolysis. The pH of the original biochar is acid neutral and may be affected by the type of feedstock.|[0085] TABLE 2|[0086] |[0087] As the temperature increases, both H, N, S, O, H/C, O/C and (O+N)/C of the sulfur-doped biochar decrease, the content of C element and ash increases, and the pH value increases, indicating that the biochar has increased alkalinity and aromaticity, and reduced oxygen-containing functional groups and polarity at high temperatures. However, the sulfur-doped biochar and the original biochar show opposite trends with respect to carbon and nitrogen content changes, and research shows that the C, N content of most biochar increases and decreases with increasing carbonization temperature, respectively, consistent with the original biochar in the comparative example of the present application. However, the reduction of the C content of the sulfur-doped biochar according to the increase of the temperature may be due to the fact that under the high temperature condition, the sulfur-containing sodium salt can react with the C element on the biochar more fully, so that the proportion of the C element is reduced, and the increase of the N content may be due to the fact that under the high temperature, more S element participates in the reaction with the biomass, so that part of N is reserved. The analysis results show that the sulfur doping and the pyrolysis temperature have great influence on the element composition of the biochar.|[0088] Table 3 shows the types and proportions of carbon-containing groups of the sulfur-doped biochar of examples 1-2 and the original biochar of comparative examples 1-2.|[0089] TABLE 3 Table 3|[0090] |[0091] After sulfur doping, only the aromatic carbon ratio in the five carbon functional groups is obviously reduced, the aromaticity is reduced, which means that S can mainly react with aromatic C, so that the content of the aromatic C is reduced, and the aromaticity is increased along with the increase of the temperature. In addition, the proportion of oxygen-containing carbon groups (carboxyl carbon and carbonyl carbon) of the biochar after sulfur doping is obviously increased, which shows that the sulfur doping introduces more oxygen-containing functional groups into the carbon structure of the biochar, the oxygen-containing carbon ratio at high temperature is reduced, and the oxygen-containing carbon ratio is consistent with the reduction of O element in element analysis.|[0092] FIG. 3 is XPS spectra of sulfur-doped biochar of examples 1-2 and raw biochar of comparative examples 1-2. From this figure, it can be seen that the S2 p peak can be detected on the biochar surface of SBC400 and SBC600, further confirming that sulfur is doped onto the biochar. Meanwhile, SBC600 has a higher level of sulfur-containing functionality on its surface than SBC400. Compared with the original biochar, the atomic percentage content of the O1s peak on the surface of the sulfur-doped biochar is obviously increased, the atomic percentage content of the C1 s peak is greatly reduced, and the same results as the elemental analysis are maintained. The significant enhancement of Ca 2p peaks on the sulfur-doped biochar surface may be due to Na 2 S 2 O 3 The sulfate radical generated by thermal decomposition reacts with calcium ions in the ash of the biochar on the surface of the biochar to generate sulfurThe precipitation of calcium acid also resulted in an increase in ash content, consistent with elemental analysis results.|[0093] Example 7|[0094] The effect detection of the sulfur-doped biochar in the soil Cr pollution remediation comprises the detection of TC, TOC, DOC, total Cr content, cr (VI) content, cr morphology and soil morphology in a soil sample.|[0095] In this example, example 5 was used as an experimental group, comparative example 3 was used as a control group, and comparative example 3 was: comparative example 3|[0096] Comparative example 3 differs from example 5 in that BC600 biochar was added at mass fractions of 1.5%, 2.5% and 3.5%, respectively.|[0097] The soil samples of example 5 and comparative example 3 were assayed for TC, TOC, DOC. The results of fig. 4 show that sulfur-doped biochar has a greater effect on DOC than original biochar and that DOC content has a significant trend of decreasing from 167mg/L to 60.6mg/L in the original soil as the addition ratio increases. As the biochar addition ratio increases, the contents of TC and TOC in the soil gradually increase. The original biochar has a very remarkable effect on increasing the content of C in the soil, the content of TC and TOC in the soil is increased from 0.750% to 2.34% at the addition amount of 3.5% to 2.50% and from 0.443% at the addition amount of 3.5% respectively, and the content of TC and TOC in the soil is increased to 1.65% to 1.34% at the addition amount of 3.5% of sulfur-doped biochar, so that the content of TC and TOC in the soil can be improved by the high carbon content of the biochar, and the carbon sequestration is facilitated. From the above, it can be seen that the sulfur-doped biochar prepared by the method can reduce the DOC dissolution of microorganism-available soil after being applied to the soil, increase the TC and TOC contents of the soil, and reduce the CO content of the soil 2 The C content and the fertility of the soil are improved at the same time of the discharge of the water-soluble carbon dioxide, and a certain carbon fixation and emission reduction effect is achieved.|[0098] The total Cr and Cr (VI) content of the soil samples of example 5 and comparative example 3 were measured by the acid leaching method. The results of FIG. 5 show that the total Cr and Cr (VI) leaching concentrations are both significantly reduced after sulfur-doped biochar is added, and gradually reduced as the stabilization time increases, the total Cr in the soil to which 2.5% SBC600 is added is reduced to 13.0mg/L in 21 days, and when the addition ratio is increased to 3.5%, the total Cr concentration has reached below the leaching toxicity standard value in 7 days, is reduced to 1.93mg/L after 21 days, and has a maximum fixation rate of 97.6% for total Cr. 3.5% of SBC600 is leached out to have a concentration of 1.20mg/L after being added into soil for 21 days, so that the requirement of solid waste leaching toxicity concentration below 5mg/L is met, the maximum fixation rate of Cr (VI) is 98.4%, and the sulfur-doped biochar material SBC600 prepared by the method has a good repairing effect on high-concentration alkaline Cr (VI) polluted soil.|[0099] After 21 days of soil culture experiments for each of the soil groups of example 5 and comparative example 3, cr morphology extraction experiments were performed. The results of fig. 6 show that the sulfur-doped biochar has a more effective positive effect on the morphological transformation of Cr in soil than the original biochar, and that the mobility of Cr is greatly reduced with the increase of the addition amount, and an effective stabilization effect is exerted on Cr.|[0100] The soil of example 5 and comparative example 3 (the mass ratio of charcoal addition was 3.5%) was subjected to morphological extraction, and the influence of the culture time on morphological changes was investigated. The results of FIG. 7 show that BC600 has less effect on the exchangeable state of Cr as the incubation time increases, while SBC600 converts the exchangeable state of Cr to an organically bound state of Cr, significantly reducing the morphology of Cr.|[0101] The Cr (VI) content of the soil samples of example 5 and comparative example 3 was measured. The results in FIG. 8 show that the Cr (VI) content in the original contaminated soil is 573mg/kg, and after SBC600 of 1.5%, 2.5% and 3.5% is added, the Cr (VI) content in the soil is 259mg/kg, 204mg/kg and 86.9mg/kg, respectively, which are reduced by 54.8%, 64.4% and 84.8%, respectively, and the restoration effect is remarkable. As the content of Cr (VI) is obviously reduced with the increase of the addition amount, the SBC600 has a good reduction effect on the Cr (VI) in the soil, wherein the reducing substance is used as an electron donor to chemically react with the Cr (VI) to generate Cr (III), and the addition ratio of 3.5% is the optimal scheme for treating the Cr-containing polluted soil.|[0102] Finally, it should be noted that the above embodiments are only for illustrating the technical solution of the present invention and not for limiting the scope of the present invention, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solution of the present invention may be modified or substituted equally without departing from the spirit and scope of the technical solution of the present invention. (CN115430401)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of biochar, and relates to sulfur-doped biochar with carbon fixation and pollution reduction effects, and a preparation method and application thereof.|BACKGROUND ART|[0002] Cr exists in the soil mainly in the form of Cr (III) and Cr (VI), where Cr (VI) is one of the most toxic pollutants in soil and water systems, is a class a carcinogen with high toxicity, mutability and teratogenicity, and is listed by the us environmental protection agency as one of the preferred pollutants in soil and water environments. In the environment, cr (VI) mainly originates from artificial activities, and a large amount of Cr (VI) is released to the environment due to wide application in chemical industries such as electroplating, tanning, pigment, corrosion prevention, metal smelting, steel manufacturing and the like, and particularly serious chromium pollution exists in soil and groundwater of industrial activity sites related to chromates. Cr (VI) is easy to migrate in soil and pore water, even spread into surface water or underground water, and is absorbed by animals and plants and generates toxic action, even the Cr (VI) is enriched into human bodies through drinking water or food chains, so that serious threat is formed to human health, and nausea, diarrhea, liver and kidney injury, dermatitis, internal bleeding and respiratory system problems can be caused under acute contact. Thus, reduction of Cr (VI) to Cr (III), reducing Cr mobility, bioavailability and toxicity is currently the primary effective method of restoring Cr (VI) soil.|[0003] The traditional soil chromium pollution restoration technology such as electrodynamic force, leaching, chemical reduction and the like has the defects of high energy consumption, high cost and secondary pollution, and the bioremediation has the limitations of long restoration period, difficult bacteria screening and the like, so that the technology is difficult to be applied to engineering practice. Development of simple, efficient, economical and environmentally friendly Cr (VI) pollution removal technology is of paramount importance. Biochar is a simple and effective soil heavy metal stabilizer, and is widely paid attention to because of the advantages of low cost, wide raw material sources, higher efficiency, less pollution and the like. Biochar is a stable carbon material generated by pyrolysis of biomass under the anoxic condition, has the characteristics of large specific surface area, high porosity, multiple surface functional groups and the like, can provide a large number of active sites, has considerable adsorption capacity, has proved that the biochar has the capacity of providing electrons, has the effect of reducing toxicity by adsorption and reduction on Cr (VI), and has potential in repairing Cr-polluted soil. Biochar also has carbon storage capacity and can reduce or inhibit CO in soil 2 Is arranged in the air. The application of the biochar can increase the content of organic carbon in the soil and generate excitation effect with the organic matters in the soil.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to overcome the defects of the prior art and provide a preparation method and application of sulfur-doped biochar with carbon fixation and pollution reduction effects.|[0005] In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:|[0006] in a first aspect, the invention provides sulfur-doped biochar, wherein the preparation raw materials of the sulfur-doped biochar comprise biomass raw materials and sodium salt containing sulfur, and the mass ratio of the biomass raw materials to the sodium salt containing sulfur is 1: (1-4);|[0007] the preparation method of the sulfur-doped biochar comprises the following steps:|[0008] s1, mixing powdered biochar raw materials with sulfur-containing sodium salt, adding water for dissolution, stirring at a constant speed, fully soaking, and drying to obtain a premix;|[0009] s2, heating the premix in the step S1 to 300-700 ℃ at a heating rate of 10 ℃/min under the anoxic condition, maintaining for 1-3h, and cooling to obtain the sulfur-doped biochar.|[0010] The powdered biochar raw material in the step S1 can be directly the powdered biochar raw material existing in the prior art, or can be self-made, and the self-made method comprises the steps of but not limited to crushing, grinding and air-drying biomass raw materials, and then sieving the biomass raw materials with a 20-mesh sieve to obtain the powdered biochar raw material; the stirring mode and the stirring time depend on the biomass raw material, for example, the biomass raw material can be stirred on a magnetic stirrer at a constant speed for 12 hours after being dissolved by adding water; drying means and drying time include, but are not limited to, placing in an oven and baking at 105 ℃ for 48 hours.|[0011] The heating mode under the anoxic condition in the step S2 includes, but is not limited to, placing the premix into a can, sealing the can, and then placing the can into a muffle furnace for heating.|[0012] The method for cleaning and removing impurities of the sulfur-doped biochar comprises the steps of, but is not limited to, cleaning the sulfur-doped biochar by high-purity water, and washing off impurities on the surface of the biochar until the conductivity of filtrate is less than or equal to 18uS/cm. Finally, the cleaned sulfur-doped biochar is dried, ground and sieved (such as a 100-mesh sieve) and then stored for later use.|[0013] The sulfur-doped biochar prepared by the method has larger specific surface area and lower functional group content. Sulfur-doped biochar with successfully introduced sulfur-containing groups (-SO) 3 H. C= S, C-S) and the oxygen-containing functional groups are increased in content, the polarity is enhanced, while biochar produced directly from biomass pyrolysis tends to contain less sulfur-containing functional groups.|[0014] As a preferred embodiment of the sulfur-doped biochar of the present invention, the mass ratio of the biomass raw material to the sulfur-containing sodium salt is 1:3.|[0015] in the invention, the too low or too high content of the sodium salt in the sulfur-containing biomass material can cause the remarkable reduction of the Cr pollution repairing effect of the prepared sulfur-doped biochar material, and the applicant discovers that the mass ratio of the biomass raw material to the sodium salt in the sulfur-containing biomass material is 1: and 3, the prepared sulfur-doped biochar material has the best effect of repairing Cr pollution.|[0016] As a preferred embodiment of the sulfur-doped biochar, the biomass raw material comprises at least one of straw, dicranopteris pedata, miscanthus and rice husk.|[0017] As a preferred embodiment of the sulfur-doped biochar of the present invention, the sulfur-containing sodium salt is Na 2 S 2 O 3 。|[0018] Molten salt method is a common strategy for preparing biochar by adopting inert salt as a sealed activating medium. The biochar prepared by the molten salt method is widely applied to the fields of environmental treatment, gas adsorption, energy storage devices and the like. The invention adopts Na as a green low-toxicity additive in molten salt medium 2 S 2 O 3 To produce S-enriched biochar, thereby effectively adsorbing heavy metals, na from soil 2 S 2 O 3 Not only is environment-friendly, but also compared with other sodium salt containing sulfur, na 2 S 2 O 3 The prepared sulfur-doped biochar material has the best effect of repairing Cr pollution.|[0019] As a preferred embodiment of the sulfur-doped biochar, the diameter of the sulfur-doped biochar is less than or equal to 0.15mm.|[0020] As a preferred embodiment of the sulfur-doped biochar of the present invention, the specific surface area of the sulfur-doped biochar is 100 to 120m 2 Per gram, the total pore volume is 0.05-0.1 cm 3 Per g, mesoporous volume > 0.04cm 3 Per gram, micropore volume of 0.01-0.05 cm 3 And/g, the average pore diameter is 2-4 nm.|[0021] In a second aspect, the invention provides a method for preparing the sulfur-doped biochar, comprising the following steps:|[0022] s1, mixing powdered biochar raw materials with sulfur-containing sodium salt, adding water for dissolution, stirring at a constant speed, fully soaking, and drying to obtain a premix;|[0023] s2, heating the premix in the step S1 to 300-700 ℃ under the anoxic condition, maintaining for 1-3h, and cooling to obtain the sulfur-doped biochar.|[0024] The preparation method provided by the invention has the advantages of high efficiency, low cost, high efficiency, stability, economy, environmental protection, high energy recovery and easiness in application, and the sulfur-doped biochar with strong adsorption capacity to Cr (VI) can be prepared at a lower temperature (300-700 ℃), so that energy consumption can be effectively reduced.|[0025] In a third aspect, the invention provides the use of the sulfur-doped biochar in the remediation of Cr contamination.|[0026] As a preferred embodiment of the application of the sulfur-doped biochar in repairing Cr pollution, the sulfur-doped biochar is applied in repairing Cr pollution of soil.|[0027] The application of the sulfur-doped biochar in repairing Cr pollution of soil comprises the following steps:|[0028] and uniformly mixing the dry polluted soil with the sulfur-doped biochar, culturing for 7-21 days, and sampling to obtain the polluted and restored soil.|[0029] The sulfur-doped biochar prepared by the method can effectively repair the Cr pollution of the soil, reduce the pH value of alkaline soil, and has good development potential in the field of repairing the Cr pollution of the soil.|[0030] As a preferred implementation mode of the application of the sulfur-doped biochar in repairing Cr pollution, the mass percentage of the sulfur-doped biochar in dry polluted soil is 1.5% -3.5%.|[0031] Compared with the prior art, the invention has the beneficial effects that:|[0032] 1. the sulfur-doped biochar prepared by the method has larger specific surface area and lower functional group content. Sulfur-doped biochar with successfully introduced sulfur-containing groups (-SO) 3 H. C= S, C-S) and the content of oxygen-containing functional groups is increased and the polarity is enhanced.|[0033] 2. The sulfur-doped biochar is prepared at a lower temperature, namely 300-700 ℃, so that the energy consumption is effectively reduced.|[0034] 3. The sulfur-doped biochar prepared by the sulfur-containing sodium salt impregnation method has strong adsorption capacity on Cr (VI).|[0035] 4. The sulfur-doped biochar prepared by the method can effectively repair Cr-polluted soil and reduce the pH value of alkaline soil.|[0036] 5. The sulfur-doped biochar prepared by the method can reduce the concentration of soluble organic carbon content (DOC) in soilIncreasing total carbon content (TC) and total organic carbon content (TOC) of soil, and reducing CO in soil 2 The C content and the fertility of the soil are improved at the same time of the discharge of the water-soluble carbon dioxide, and a certain carbon fixation and emission reduction effect is achieved.|[0037] 6. The sulfur-doped biochar prepared by the method can be used as a repair material with high efficiency, low cost and environmental friendliness, and has good development potential in the field of Cr pollution repair.|DRAWINGS DESCRIPTION|[0038] FIG. 1 is an electron scanning microscope (SEM) morphology diagram and an EDS-Mapping diagram of the sulfur-doped biochar material prepared by the method.|[0039] FIG. 2 shows adsorption-desorption curves (a) and pore size distribution diagrams (b) of sulfur-doped biochar materials prepared by the method.|[0040] FIG. 3 is an XPS spectrum of the sulfur-doped biochar material prepared by the invention.|[0041] Fig. 4 is a graph showing the variation of DOC, TC and TOC in soil after soil remediation experiments using the sulfur-doped biochar material SBC600 and the original biochar BC600 prepared by the present invention.|[0042] Fig. 5 is a graph showing the change of the acid leaching concentration of (a) total Cr and (b) Cr (VI) in soil after a soil remediation experiment is performed by using the sulfur-doped biochar material SBC600 and the original biochar BC600 prepared by the method.|[0043] FIG. 6 is a graph showing the effect of different amounts of added sulfur-doped biochar material SBC600 and original biochar BC600 on the morphological change of Cr in soil.|[0044] FIG. 7 is a graph showing the effect of SBC600 and BC600 of sulfur-doped biochar material prepared by the invention on the morphological change of Cr in soil under different culture times.|[0045] FIG. 8 is a graph showing the variation of Cr (VI) content in soil after repairing Cr-contaminated soil by using the sulfur-doped biochar material SBC600 and the original biochar BC600 prepared by the method.|INVENTION MODE|Detailed Description|[0046] For a better description of the objects, technical solutions and advantages of the present invention, the present invention will be further described with reference to the following specific examples.|[0047] Example 1|[0048] The preparation method of the sulfur-doped biochar comprises the following steps:|[0049] (1) Pulverizing radix Osmundae, grinding, air drying, and sieving with 20 mesh sieve to obtain radix Osmundae powder.|[0050] (2) Na is mixed with 2 S 2 O 3 Mixing with the dicranopteris pedata powder according to the ratio of 3:1, adding water for dissolution, stirring for 12 hours at a constant speed on a magnetic stirrer, fully soaking, and then placing into a baking oven for baking at 105 ℃ for 48 hours until drying, thus obtaining the pre-mixed dicranopteris pedata powder after soaking.|[0051] (3) And (3) placing the immersed dicranopteris pedata powder premix into an iron tank to be sealed and placed into a muffle furnace, and heating to 600 ℃ at a heating rate of 10 ℃/min for 1h to obtain the high-temperature sulfur-doped biochar (SBC 600).|[0052] (4) And taking out the sulfur-doped biochar after the sulfur-doped biochar is naturally cooled, and cleaning the sulfur-doped biochar by using high-purity water to remove impurities on the surface of the sulfur-doped biochar until the conductivity of filtrate is less than or equal to 18uS/cm. Finally, the cleaned sulfur-doped biochar is dried, ground and sieved by a 100-mesh sieve for later use.|[0053] The electron scanning microscope (SEM) topography and EDS-Mapping of SBC600 were tested by conventional means in the art, and the results are shown in fig. 1, by which it was possible to observe that the S element was uniformly dispersed on the surface of SBC600, strongly demonstrating that S was doped into the biochar matrix.|[0054] Example 2|[0055] Example 2 differs from example 1 in that the sulfur-doped biochar (SBC 400) was heated to 400℃at a heating rate of 10℃per minute for 1 hour, i.e., a low temperature.|[0056] Example 3|[0057] The preparation method of the sulfur-doped biochar comprises the following steps:|[0058] (1) And (3) crushing, grinding and air-drying the straw, and sieving the crushed straw with a 20-mesh sieve to obtain straw powder.|[0059] (2) Na is mixed with 2 S 2 O 3 Mixing the powder with straw powder according to the ratio of 1:1, adding water for dissolution, stirring on a magnetic stirrer at a constant speed for 12 hours, fully soaking, and then putting into a baking oven for baking at 105 ℃ for 48 hours until the straw powder is dried, thus obtaining the soaked straw powder premix.|[0060] (3) And (3) placing the immersed straw powder premix into a steel pot, sealing and loading into a muffle furnace, and heating to 700 ℃ at a heating rate of 10 ℃/min for 3 hours to obtain the high-temperature sulfur-doped biochar (SBC 700).|[0061] (4) And taking out the sulfur-doped biochar after the sulfur-doped biochar is naturally cooled, and cleaning the sulfur-doped biochar by using high-purity water to remove impurities on the surface of the sulfur-doped biochar until the conductivity of filtrate is less than or equal to 18uS/cm. Finally, the cleaned sulfur-doped biochar is dried, ground and sieved by a 100-mesh sieve for later use.|[0062] Example 4|[0063] The preparation method of the sulfur-doped biochar comprises the following steps:|[0064] (1) Crushing, grinding and air-drying the miscanthus sinensis, and sieving with a 20-mesh sieve to obtain miscanthus sinensis powder.|[0065] (2) Na is mixed with 2 S 2 O 3 Mixing with the miscanthus powder according to the ratio of 4:1, adding water, dissolving, stirring on a magnetic stirrer at a constant speed for 12h, fully soaking, and then placing into a baking oven to bake at 105 ℃ for 48h until drying to obtain the soaked miscanthus powder premix.|[0066] (3) And (3) placing the soaked miscanthus powder premix into an iron pot, sealing and loading into a muffle furnace, and heating to 300 ℃ at a heating rate of 10 ℃/min for 1h to obtain the low-temperature sulfur-doped biochar (SBC 300).|[0067] (4) And taking out the sulfur-doped biochar after the sulfur-doped biochar is naturally cooled, and cleaning the sulfur-doped biochar by using high-purity water to remove impurities on the surface of the sulfur-doped biochar until the conductivity of filtrate is less than or equal to 18uS/cm. Finally, the cleaned sulfur-doped biochar is dried, ground and sieved by a 100-mesh sieve for later use.|[0068] The electron scanning microscope (SEM) topography and EDS-Mapping of examples 2-4 were similar to example 1, demonstrating that S was doped into the biochar matrix.|[0069] Example 5|[0070] An embodiment of the application of sulfur-doped biochar in Cr pollution in the invention, the application of sulfur-doped biochar in soil Cr pollution remediation in the embodiment comprises the following steps:|[0071] 40g of polluted soil is weighed, SBC600 with mass fractions of 1.5%, 2.5% and 3.5% is respectively added, 4 parallel treatments are arranged for each treatment, the dried soil and the SBC600 are uniformly mixed, then the mixture is cultivated in a climatic chamber, the constant temperature is set to 20.0 ℃, the relative humidity is set to 65%, and the samples are respectively taken on days 7, 14 and 21 to obtain the polluted repair soil. Soil moisture needs to be maintained at 60% of the field capacity of the soil during cultivation.|[0072] Example 6|[0073] An embodiment of the performance comparison of the sulfur-doped biochar and the original biochar comprises the comparison of biochar to N 2 Adsorption-desorption, pore size distribution, specific surface area, elemental composition, pH, type of carbon-containing groups and comparison of ratios.|[0074] In this example, examples 1 to 2 were used as experimental groups, comparative examples 1 to 2 were used as control groups, and comparative examples 1 to 2 were respectively:|[0075] comparative example 1|[0076] Comparative example 1 was different from example 1 in that the non-impregnated powder of dicranopteris pedata was placed in a retort and sealed in a muffle furnace to prepare high-temperature raw biochar (BC 600).|[0077] Comparative example 2|[0078] Comparative example 2 was different from example 2 in that the non-impregnated powder of dicranopteris pedata was placed in a retort and sealed in a muffle furnace to prepare a low-temperature raw biochar (BC 400).|[0079] FIG. 2 shows the pair N of sulfur-doped biochar of examples 1-2 and the original biochar of comparative examples 1-2 2 The adsorption-desorption curve of SBC600 is IV type, and H4 hysteresis appears under relatively high pressure, which indicates that the biochar is mesoporous biochar, the mesoporous volume of the biochar accounts for 66.2% of the total pore volume, and the average pore diameter is 2.51nm.|[0080] Table 1 shows BET specific surface areas of sulfur-doped biochars of examples 1 to 2 and original biochars of comparative examples 1 to 2.|[0081] TABLE 1|[0082] |[0083] As can be seen from Table 1, the specific surface area of SBC400 is 114m 2 Specific surface area of SBC600 is 109m 2 Per g, the increase of the specific surface area at low temperature after sulfur incorporation is probably due to the generation of sulfur-containing gas (H) at 300℃to 400 ℃ 2 S、SO 2 、CS 2 Etc.), thereby forming more pore structures. The specific surface area is probably reduced at high temperature because the salt is added to block the micropores, and the decomposition of the salt at high temperature and the functional group formed by the reaction on the surface of the biochar destroy the micropore structure, so that more reactive sites are provided for the surface of the biochar.|[0084] Table 2 shows elemental composition analysis and pH values of sulfur-doped biochar of examples 1 to 2 and the original biochar of comparative examples 1 to 2. The modified SBC600 had a sulfur content increased to 19.8%, again demonstrating successful sulfur incorporation. Compared with the original biochar, after sulfur doping, the contents of C, H and N elements and the pH value are reduced, the ash content, the ratio of O/C to (O+N)/C are increased, and the effects that the oxygen-containing functional group content of the sulfur-doped biochar is increased, the hydrophilicity and the polarity are enhanced, and the S atoms have higher electron gravity and can increase the surface polarity of the biochar are shown. The pH of the biochar is an indicator of the number of surface acidity or basic functional groups, and the acidity of sulfur-doped biochar may be caused by the generation of more acidic groups on the surface of the biochar during pyrolysis. The pH of the original biochar is acid neutral and may be affected by the type of feedstock.|[0085] TABLE 2|[0086] |[0087] As the temperature increases, both H, N, S, O, H/C, O/C and (O+N)/C of the sulfur-doped biochar decrease, the content of C element and ash increases, and the pH value increases, indicating that the biochar has increased alkalinity and aromaticity, and reduced oxygen-containing functional groups and polarity at high temperatures. However, the sulfur-doped biochar and the original biochar show opposite trends with respect to carbon and nitrogen content changes, and research shows that the C, N content of most biochar increases and decreases with increasing carbonization temperature, respectively, consistent with the original biochar in the comparative example of the present application. However, the reduction of the C content of the sulfur-doped biochar according to the increase of the temperature may be due to the fact that under the high temperature condition, the sulfur-containing sodium salt can react with the C element on the biochar more fully, so that the proportion of the C element is reduced, and the increase of the N content may be due to the fact that under the high temperature, more S element participates in the reaction with the biomass, so that part of N is reserved. The analysis results show that the sulfur doping and the pyrolysis temperature have great influence on the element composition of the biochar.|[0088] Table 3 shows the types and proportions of carbon-containing groups of the sulfur-doped biochar of examples 1-2 and the original biochar of comparative examples 1-2.|[0089] TABLE 3 Table 3|[0090] |[0091] After sulfur doping, only the aromatic carbon ratio in the five carbon functional groups is obviously reduced, the aromaticity is reduced, which means that S can mainly react with aromatic C, so that the content of the aromatic C is reduced, and the aromaticity is increased along with the increase of the temperature. In addition, the proportion of oxygen-containing carbon groups (carboxyl carbon and carbonyl carbon) of the biochar after sulfur doping is obviously increased, which shows that the sulfur doping introduces more oxygen-containing functional groups into the carbon structure of the biochar, the oxygen-containing carbon ratio at high temperature is reduced, and the oxygen-containing carbon ratio is consistent with the reduction of O element in element analysis.|[0092] FIG. 3 is XPS spectra of sulfur-doped biochar of examples 1-2 and raw biochar of comparative examples 1-2. From this figure, it can be seen that the S2 p peak can be detected on the biochar surface of SBC400 and SBC600, further confirming that sulfur is doped onto the biochar. Meanwhile, SBC600 has a higher level of sulfur-containing functionality on its surface than SBC400. Compared with the original biochar, the atomic percentage content of the O1s peak on the surface of the sulfur-doped biochar is obviously increased, the atomic percentage content of the C1 s peak is greatly reduced, and the same results as the elemental analysis are maintained. The significant enhancement of Ca 2p peaks on the sulfur-doped biochar surface may be due to Na 2 S 2 O 3 The sulfate radical generated by thermal decomposition reacts with calcium ions in the ash of the biochar on the surface of the biochar to generate sulfurThe precipitation of calcium acid also resulted in an increase in ash content, consistent with elemental analysis results.|[0093] Example 7|[0094] The effect detection of the sulfur-doped biochar in the soil Cr pollution remediation comprises the detection of TC, TOC, DOC, total Cr content, cr (VI) content, cr morphology and soil morphology in a soil sample.|[0095] In this example, example 5 was used as an experimental group, comparative example 3 was used as a control group, and comparative example 3 was: comparative example 3|[0096] Comparative example 3 differs from example 5 in that BC600 biochar was added at mass fractions of 1.5%, 2.5% and 3.5%, respectively.|[0097] The soil samples of example 5 and comparative example 3 were assayed for TC, TOC, DOC. The results of fig. 4 show that sulfur-doped biochar has a greater effect on DOC than original biochar and that DOC content has a significant trend of decreasing from 167mg/L to 60.6mg/L in the original soil as the addition ratio increases. As the biochar addition ratio increases, the contents of TC and TOC in the soil gradually increase. The original biochar has a very remarkable effect on increasing the content of C in the soil, the content of TC and TOC in the soil is increased from 0.750% to 2.34% at the addition amount of 3.5% to 2.50% and from 0.443% at the addition amount of 3.5% respectively, and the content of TC and TOC in the soil is increased to 1.65% to 1.34% at the addition amount of 3.5% of sulfur-doped biochar, so that the content of TC and TOC in the soil can be improved by the high carbon content of the biochar, and the carbon sequestration is facilitated. From the above, it can be seen that the sulfur-doped biochar prepared by the method can reduce the DOC dissolution of microorganism-available soil after being applied to the soil, increase the TC and TOC contents of the soil, and reduce the CO content of the soil 2 The C content and the fertility of the soil are improved at the same time of the discharge of the water-soluble carbon dioxide, and a certain carbon fixation and emission reduction effect is achieved.|[0098] The total Cr and Cr (VI) content of the soil samples of example 5 and comparative example 3 were measured by the acid leaching method. The results of FIG. 5 show that the total Cr and Cr (VI) leaching concentrations are both significantly reduced after sulfur-doped biochar is added, and gradually reduced as the stabilization time increases, the total Cr in the soil to which 2.5% SBC600 is added is reduced to 13.0mg/L in 21 days, and when the addition ratio is increased to 3.5%, the total Cr concentration has reached below the leaching toxicity standard value in 7 days, is reduced to 1.93mg/L after 21 days, and has a maximum fixation rate of 97.6% for total Cr. 3.5% of SBC600 is leached out to have a concentration of 1.20mg/L after being added into soil for 21 days, so that the requirement of solid waste leaching toxicity concentration below 5mg/L is met, the maximum fixation rate of Cr (VI) is 98.4%, and the sulfur-doped biochar material SBC600 prepared by the method has a good repairing effect on high-concentration alkaline Cr (VI) polluted soil.|[0099] After 21 days of soil culture experiments for each of the soil groups of example 5 and comparative example 3, cr morphology extraction experiments were performed. The results of fig. 6 show that the sulfur-doped biochar has a more effective positive effect on the morphological transformation of Cr in soil than the original biochar, and that the mobility of Cr is greatly reduced with the increase of the addition amount, and an effective stabilization effect is exerted on Cr.|[0100] The soil of example 5 and comparative example 3 (the mass ratio of charcoal addition was 3.5%) was subjected to morphological extraction, and the influence of the culture time on morphological changes was investigated. The results of FIG. 7 show that BC600 has less effect on the exchangeable state of Cr as the incubation time increases, while SBC600 converts the exchangeable state of Cr to an organically bound state of Cr, significantly reducing the morphology of Cr.|[0101] The Cr (VI) content of the soil samples of example 5 and comparative example 3 was measured. The results in FIG. 8 show that the Cr (VI) content in the original contaminated soil is 573mg/kg, and after SBC600 of 1.5%, 2.5% and 3.5% is added, the Cr (VI) content in the soil is 259mg/kg, 204mg/kg and 86.9mg/kg, respectively, which are reduced by 54.8%, 64.4% and 84.8%, respectively, and the restoration effect is remarkable. As the content of Cr (VI) is obviously reduced with the increase of the addition amount, the SBC600 has a good reduction effect on the Cr (VI) in the soil, wherein the reducing substance is used as an electron donor to chemically react with the Cr (VI) to generate Cr (III), and the addition ratio of 3.5% is the optimal scheme for treating the Cr-containing polluted soil.|[0102] Finally, it should be noted that the above embodiments are only for illustrating the technical solution of the present invention and not for limiting the scope of the present invention, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solution of the present invention may be modified or substituted equally without departing from the spirit and scope of the technical solution of the present invention. Family Number|(102897237)|102897237|Abstract|(CN115430401B B)|The invention relates to sulfur - doped biochar with both carbon sequestration and pollution reduction effects as well as a preparation method and application thereof , and belongs to the technical field of biochar . The preparation method of the sulfur - doped biochar with both carbon sequestration and pollution reduction effects comprises the following steps : crushing , grinding and air - drying a biomass raw material , sieving to obtain a powdery biochar precursor , mixing the powdery biochar precursor with a sulfur - containing sodium salt , adding water for dissolving , stirring at a constant speed , fully dipping , and heating in a muffle furnace to obtain the sulfur - doped biochar . The sulfur - doped biochar material is low in price , simple to prepare and good in stability , and compared with original biochar , the sulfur - doped biochar not only has a carbon sequestration effect , but also has a remarkable remediation effect on Cr - polluted soil . |CPC codes|(CN115430401B B)|B01J - 020/02/66 |B01J - 020/20 |B01J - 020/30/78 |IPC codes|(CN115430401B B)|B01J - 020/20 |B01J - 020/30 |Title|(CN115430401 A)|Sulfur - doped biochar with carbon sequestration and pollution reduction effects as well as preparation method and application of sulfur - doped biochar | Chemical engineering|Environmental technology B01J-020/02/66|B01J-020/20|B01J-020/30/78|B09C-001/00 B01J-020/02/66|B01J-020/20|B01J-020/30/78|B09C-001/00 B01J-020/20|B01J-020/30|B09C-001/00 B01J-020/20|B01J-020/30|B09C-001/00 WO2024229280|CN117139354B|US12497565 WO2024229280 112086086 WHO=Examiner SELF=N CAT=A|CN117139354B 107577234 WHO=Examiner SELF=N|US12497565 107946232 WHO=Applicant SELF=N CN113600127|CN114702975|CN113856621|CN109896627|US20140102978|US20170282229 CN113600127 96856537 WHO=Examiner SELF=N CAT=Y|CN114702975 100737886 WHO=Examiner SELF=N CAT=A|CN113856621 97954553 WHO=Examiner SELF=N CAT=A|CN109896627 84894864 WHO=Examiner SELF=N CAT=A|US20140102978 65178043 WHO=Examiner SELF=N CAT=A|US20170282229 68732820 WHO=Examiner SELF=N US20140102978; CN109896627; CN113600127; CN113856621; CN114702975; US20170282229 (CN115430401)|Search Report references [Examiner]|-YIN MENGMENG ET AL.: "Sulfur-functional group tunning on biochar through sodium thiosulfate modified molten salt process for efficient heavy metal adsorption", pages 2| GRANTED (CN115430401)|GRANTED ALIVE (CN115430401)|ALIVE (CN115430401)|LEGAL DETAILS FOR CN115430401|Actual or expected expiration date=2042-09-23|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-09-23|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211169882|Application date=2022-09-23|Standardized application number=2022CN-1169882|Event publication date=2022-12-06|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115430401|Publication stage code=A|Publication date=2022-12-06|Standardized publication number=CN115430401|Event publication date=2022-12-06|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-12-23|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-06-23|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN115430401|Publication stage code=B|Publication date=2023-06-23|Standardized publication number=CN115430401B|Event publication date=2023-06-23|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN115430401)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQ4lP/kxCYXoxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000068314884&ekey=2159&xpn=CN115430401B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=AVK5rYeqoQB0%252B5pEshF3GbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN115430401)|CN|(CN115430401)|CN (CN115430401)|NAME=SUN YAT-SEN UNIVERSITY , COUNTRY=CN|(CN115430401)|NAME=SUN YAT-SEN UNIVERSITY , COUNTRY=CN (CN115430401)|NAME=CHEN JING;SCIHEAD IP LAW FIRM , REG=44202|(CN115430401)|NAME=CHEN JING;SCIHEAD IP LAW FIRM , REG=44202 (CN115430401)|NAME=ZHAO NAN|NAME=LUO QIAN|NAME=YANG ZAIKUAN|NAME=LIU KUNYUAN|NAME=XU QIANTING|NAME=ZHANG WEIHUA|NAME=CHOU RONGLIANG|(CN115430401)|NAME=ZHAO NAN|NAME=LUO QIAN|NAME=YANG ZAIKUAN|NAME=LIU KUNYUAN|NAME=XU QIANTING|NAME=ZHANG WEIHUA|NAME=CHOU RONGLIANG 0 1 Titre: (CN115430401)|Sulfur-doped biochar with carbon fixation and pollution reduction effects as well as preparation method and application thereof Résumé: (CN115430401)|The invention relates to sulfur-doped biochar with both carbon sequestration and pollution reduction effects as well as a preparation method and application thereof, and belongs to the technical field of biochar. The preparation method of the sulfur-doped biochar with both carbon sequestration and pollution reduction effects comprises the following steps: crushing, grinding and air-drying a biomass raw material, sieving to obtain a powdery biochar precursor, mixing the powdery biochar precursor with a sulfur-containing sodium salt, adding water for dissolving, stirring at a constant speed, fully dipping, and heating in a muffle furnace to obtain the sulfur-doped biochar. The sulfur-doped biochar material is low in price, simple to prepare and good in stability, and compared with original biochar, the sulfur-doped biochar not only has a carbon sequestration effect, but also has a remarkable remediation effect on Cr-polluted soil. 34 Abstract gpt-4o-mini no The article focuses on sulfur-doped biochar for carbon sequestration and pollution reduction, which does not involve the accelerated weathering of silicate or alkaline minerals for CO₂ capture.
34 CN202211564985 CN202211564985 CN115728223 103959807 CN115728223 A 2023-03-03 [CN115728223] 2022-12-07 2022-12-07 2023-03-03 (CN115728223)|2042-12-07 (CN115728223)|Carbon sequestration capability assessment method, device and system based on watershed scale karst weathering, and medium (CN115728223)|The invention is suitable for the technical field of carbon sink monitoring, and provides a carbon sink capacity assessment method, device and system based on watershed scale karst weathering and a medium. Acquiring real-time hydrological information; acquiring real-time water quality information; calculating the CO2 consumption flux; calculating the carbon sink strength; the device comprises a drainage basin division module; a monitoring section setting module; a data acquisition module; a data processing module; and an evaluation module. The invention creatively provides the carbon sink capacity assessment method, device and system based on the drainage basin scale karst weathering and the medium, and provides a new research direction for dynamic monitoring and quantitative calculation in the karst carbon sink weathering process. The hydrological information data and the water quality information data can be continuously collected and processed in real time, synchronous and high-resolution data are obtained, and the timeliness and accuracy of carbon sink capacity evaluation can be effectively guaranteed. CHONGQING ECOLOGICAL ENV MONITORING CENTER (CN115728223)|CHONGQING ECOLOGICAL ENV MONITORING CENTER ([CN]) QIN CHENG|DENG LI|LIU HAO|LIU NIAN|CAI YU|GE MIAO|YANG BING|HU QIYAO|GONG LI|JIANG JING|TANG XIAO|YU HANG (CN115728223)|QIN CHENG|DENG LI|LIU HAO|LIU NIAN|CAI YU|GE MIAO|YANG BING|HU QIYAO|GONG LI|JIANG JING|TANG XIAO|YU HANG (CN115728223)|XU WEIWEI;CHONGQING XINHANG INTELLECTUAL PROPERTY AGENCY CO. LTD.|Reg. Nb: 50218 (CN115728223)|Compared with the prior art, the invention has the advantages and positive effects that: the invention creatively provides a carbon sink capacity evaluation method, device, system and medium based on watershed scale karst weathering, and provides a new research direction for dynamic monitoring and quantitative calculation in the karst carbon sink weathering process.| (CN115728223)|1. A carbon sink capacity evaluation method based on watershed scale karst weathering is characterized by comprising the following steps: the method comprises the following steps:s1, selecting a monitoring section: selecting an outlet section of the drainage basin as a monitoring section, wherein the drainage basin comprises: rivers with a defined watershed range and rivers without a defined watershed range;s2, acquiring real-time hydrological information: the hydrologic information includes: the cross section area, the cross section flow, the water flow velocity, the water surface elevation and the water flow direction;s3, acquiring real-time water quality information: the water quality information comprises: pH value, water temperature, HCO 3- Concentration;s4, calculating CO 2 Consumption flux: the hydrological information and the water quality information are combined, and the CO is calculated by utilizing an integral mode 2 Consuming the flux;s5, calculating the carbon sink strength: binding of CO 2 The carbon sink strength was calculated from the consumed flux and the basin area.|7. The utility model provides a carbon sink ability evaluation device based on basin scale karst weathering which characterized in that: the method comprises the following steps:the drainage basin dividing module adopts a GIS technology, and performs river network extraction and catchment unit division based on digital elevation model data to finish drainage basin division;the monitoring section setting module is used for fusing the distribution conditions of the existing automatic water quality monitoring stations and hydrological stations and automatically screening the monitoring sections;the data acquisition module is used for acquiring hydrological information and water quality information, the hydrological information comprises but is not limited to section area, section flow, water flow speed, water surface elevation and water flow direction, and the water quality information comprises but is not limited to pH value, water temperature and HCO 3- Concentration;the data processing module is used for matching effective hydrological information and water quality information data, deleting redundant and abnormal data and calculating HCO 3- Ion flux, CO 2 Consuming the flux;and the evaluation module generates a karst carbon sink strength report of the watershed scale.| (CN115728223)|The invention creatively provides a carbon sink capacity evaluation method, device, system and medium based on watershed scale karst weathering, and provides a new research direction for dynamic monitoring and quantitative calculation in the karst carbon sink weathering process.|The invention relates to the technical field of carbon sink monitoring, in particular to a method, a device, a system and a medium for evaluating carbon sink capacity based on drainage basin scale karst weathering.| (CN115728223)|CARBON SINK(100,60)|WATERSHED(100,31)|CAPACITY EVALUATION(100,20)|CARBON SINK CAPACITY EVALUATION(100,17)|KARSTIC WEATHERING(100,7)|MEDIUM(100,7)|BASIN(100,6)|ABILITY EVALUATION(100,2)|CARBON SINK ABILITY EVALUATION(100,2)|KARST WEATHERING(100,1)|HYDROLOGICAL INFORMATION(88,23)|QUANTITATIVE CALCULATION(82,2)|HYDROLOGICAL SLICE(68,11)|CARBON SEQUESTRATION CAPACITY ASSESSMENT(67,7)|DYNAMIC MONITORING(61,2)|KARST CARBON SINK(56,8)|HYDROLOGICAL STATION(54,8)|DRAINAGE BASIN DIVIDING MODULE(50,4)|DRAINAGE BASIN(47,15)|FLUX CONSUMPTION(47,6)|EVALUATION MODULE(47,5)|CALCULATING HCO(46,3)|CONSUMPTION FLUX(43,7)|CATCHMENT UNIT DIVISION(41,1)|DRAINAGE BASIN DIVISION(39,3)|WATERSHED SCALE(39,3)|MONITORING SECTION(35,29)|WATERSHED RANGE(35,5)|MONITORING CARBON SINK(35,2)|HYDROLOGIC INFORMATION(34,3)|RIVER(31,13)|CARBON SINK STRENGTH(31,12)|FLUX(31,11)|DIVIDING MODULE(31,4)|HCO CALCULATION(29,3)|REDUNDANT DATA(27,3)|CARBON SINK CAPACITY(26,3)|WATER QUALITY INFORMATION(24,23)|DATA ACQUISITION MODULE(23,6)|BASIN AREA(22,6)|ABNORMAL DATA(22,3)|RADAR WAVE(22,3)|HCO(21,18)|CARBON SINK CAPACITY ASSESSMENT(21,2)|BASIN CARBON SINK(20,5)|ACOUSTIC DOPPLER CURRENT METER(20,4)|PERIOD HCO(20,1)|MULTICHANNEL ION POTENTIOMETER(19,5)|HYDROLOGICAL INFORMATION DATA(19,2)|TIMELINESS(19,2)|WATER QUALITY SLICE(18,11)|PH VALUE(18,6)|OUTLET SECTION(17,6)|ULTRASONIC PROBE(15,3)|WEATHERING(15,2)|STORAGE MEDIUM(15,1)|DATA ACQUISITION(13,6)|DATA PROCESSING MODULE(12,6)|PUZI RIVER BASIN(12,2)|KARST BIG COUNTRY(12,1)|AUTOMATIC WATER QUALITY MONITORING(10,8)|GAS SENSITIVE ELECTRODE(10,5)|HYDROLOGIC SITE(10,2)|DRAINAGE BASIN OUTLET SECTION(9,6)|REALTIME ACQUISITION(9,5)|DIGITAL ELEVATION MODEL DATA(9,3)|CONTAMINATED WATERSHED(9,1)|KARST CO2 CONSUMPTION(9,1)|WEATHERING CO2 CONSUMPTION(9,1)|WATER QUALITY INFORMATION DATA(8,5)|DIGITAL ELEVATION MODEL(8,4)|CARBON SEQUESTRATION CAPACITY EVALUATION(8,3)|LABORATORY ANALYSIS(8,3)|IMMEDIATE REPORT(8,2)|RIVER NETWORK(8,2)|HYDROLOGY SLICE(8,1)|ORDINARY RIVER MOUTH(8,1)|REGULAR RIVER BED(8,1)|RIVER HCO(8,1)|AVERAGE DISTANCE AVERAGE VALUE(7,6)|PH ELECTRODE(7,4)|WATER FLOW VELOCITY(7,4)|AVERAGE FLOW(7,3)|ION SELECTIVE ELECTRODE(7,3)|SECTION FLOW(7,3)|WATER SURFACE ELEVATION(7,3)|ACQUISITION HYDROLOGICAL INFORMATION(7,1)|AUTOMATIC WATERSHED DIVISION(7,1)|CLOUD SERVER(7,1)|CO2 CONSUMPTION FLUX(7,1)|DRAINAGE BASIN MINERAL WEATHERING(7,1)|FLOW SPEED(7,1)|GLOBAL CARBON NEUTRALIZATION(7,1)|ONLINE MONITORING(7,1)|SCIENTIFIC MONITORING(7,1)|ULTRASONICTHE WAVE(7,1)|WATER TEMPERATURE(6,11)|COMMUNICATION UNIT(6,9)|DATA COMMUNICATION(6,7)|DATA PROCESSING(6,6)|EQUIVALENT RATIO(6,6)|CARBON DIOXIDE(6,5)|WATER SURFACE(6,4)|GEOLOGICAL CARBON SINK(6,2)|CARBON NEUTRALIZATION TARGET(6,1)|CATCHMENT RELATION(6,1)|ETHERNET MODULE(6,1)|EXOGENOUS ACID INFLUENCE(6,1)|HYDROLOGY SITE(6,1)|INSTRUCTION SEGMENT(6,1)|KARST CARBON SINK CAPABILITY(6,1)|KARST CARBON SINK EVALUATION(6,1)|MASTER CONTROL(6,1)|OPERATOR ANALYZED CA(6,1)|TFT DISPLAY SCREEN(6,1)|WIFI MODULE(6,1)|WIRELESS COMMUNICATION MODULE(6,1)|DIVISION AREA(5,3)|CALCIUM ION ELECTRODE(5,2)|CONCENTRATION TIME(5,2)|WATERSHED AREA(5,2)|WATER FLOW DIRECTION(4,6)|FUNCTIONAL UNIT(4,4)|CONSTANT NUMBER(4,3)|MG L(4,3)|ULTRASOUND(4,3)|ARM FRAMEWORK(4,1)|ECOLOGICAL CIVILIZATION CONSTRUCTION CONTENT(4,1)|ION CHROMATOGRAPHY(4,1)|MONITORING ACCURACY(4,1)|OCEAN CARBON SINK(4,1)|ORDINARY MEANING(4,1)|PRACTICABILITY(4,1)|PUZI RIVER LENGTH(4,1)|SHALLOW RIVER CHANNEL(4,1)|SOLUBLE ROCK(4,1)|SPECTROPHOTOMETER(4,1)|STRENGTH CALCULATION(4,1)|WATERSHED CARBON SINK(4,1)| (CN115728223)|1. A carbon sink capacity evaluation method based on watershed scale karst weathering is characterized by comprising the following steps: the method comprises the following steps:|s1, selecting a monitoring section: selecting an outlet section of the drainage basin as a monitoring section, wherein the drainage basin comprises: rivers with a defined watershed range and rivers without a defined watershed range;|s2, acquiring real-time hydrological information: the hydrologic information includes: the cross section area, the cross section flow, the water flow velocity, the water surface elevation and the water flow direction;|s3, acquiring real-time water quality information: the water quality information comprises: pH value, water temperature, HCO 3- Concentration;|s4, calculating CO 2 Consumption flux: the hydrological information and the water quality information are combined, and the CO is calculated by utilizing an integral mode 2 Consuming the flux;|s5, calculating the carbon sink strength: binding of CO 2 The carbon sink strength was calculated from the consumed flux and the basin area.|2. The carbon sequestration capacity assessment method based on watershed scale karstic weathering as claimed in claim 1, characterized in that:|s1 further comprises: and selecting a drainage basin outlet section which is superposed with the existing hydrological station or automatic water quality monitoring station as a monitoring section.|3. The carbon sequestration capacity assessment method based on watershed scale karstic weathering as claimed in claim 1, characterized in that:|s2 further comprises: acquiring the hydrological information by selecting any one of an acoustic Doppler principle, an ultrasonic time difference method and a radar wave principle;|s3 further comprises: HCO calculation by ion selective electrode method 3- Concentration, the formula is as follows:|wherein, K 1 、K 2 Is a constant number, C T Is water temperature, [ H ] + ]Is represented by H + The ion concentration.|4. The carbon sequestration capacity assessment method based on watershed scale karstic weathering as claimed in claim 1, characterized in that:|s3 further comprises: and monitoring points for acquiring water quality information are uniformly distributed along the outlet section of the basin.|5. The carbon sequestration capacity assessment method based on watershed scale karstic weathering as claimed in claim 1, characterized in that:|s4, further comprising:|CO 2 the formula for the consumed flux is as follows:|W=∫ T F(t)dt=∫ T Q(t)C(t)dt=Q a C a T+∫ T Q″C″d|F=W x 44/(2 x 61)|wherein W is HCO 3- Ion flux (g/s), Q a Is the time-interval average flow (m) 3 /s),C a Is period HCO 3- Average concentration (mg/L), T is an estimation time period, Q 'is a flow time average distance average value, and C' is a concentration time average distance average value; f is CO 2 Flux (g/s) was consumed.|6. The carbon sink capacity evaluation method based on watershed scale karst weathering as claimed in claim 1, wherein:|s5, further comprising:|the carbon sink strength is calculated as follows:|I=F/K|wherein I is the basin carbon sink strength (t/km) 2 A); f is CO 2 Consumption flux (t/a); k is the basin area (km) 2 )。|7. The invention provides a carbon sink ability evaluation device based on basin scale karst weathering which characterized in that: the method comprises the following steps:|the drainage basin dividing module adopts a GIS technology, and performs river network extraction and catchment unit division based on digital elevation model data to finish drainage basin division;|the monitoring section setting module is used for fusing the distribution conditions of the existing automatic water quality monitoring stations and hydrological stations and automatically screening the monitoring sections;|the data acquisition module is used for acquiring hydrological information and water quality information, the hydrological information comprises but is not limited to section area, section flow, water flow speed, water surface elevation and water flow direction, and the water quality information comprises but is not limited to pH value, water temperature and HCO 3- Concentration;|the data processing module is used for matching effective hydrological information and water quality information data, deleting redundant and abnormal data and calculating HCO 3- Ion flux, CO 2 Consuming the flux;|and the evaluation module generates a karst carbon sink strength report of the watershed scale.|8. A carbon sink ability evaluation system based on watershed scale karst weathering is characterized in that: the system comprises a main control unit, an acquisition unit, a storage unit, a communication unit and a power supply unit;|the storage unit is used for storing a computer program;|the master control unit comprises a processor, which when executing the computer program, is capable of implementing the method for assessing the carbon sequestration capacity based on watershed-scale karstic weathering as claimed in any one of claims 1 to 6;|the acquisition unit comprises a hydrological monitor for acquiring hydrological information and a water quality monitor for acquiring water quality information, and the hydrological monitor and the water quality monitor are in data communication with the processor;|the communication unit is used for realizing data communication between the processor and the background;|the power supply unit is used for supplying power to each functional unit.|9. The carbon sequestration capacity assessment system based on watershed scale karst weathering as claimed in claim 8, wherein:|the hydrological monitor is an acoustic Doppler current meter which is connected with a plurality of ultrasonic probes;|the water quality monitor adopts a multi-channel ion potentiometer which is connected with a pH electrode and a carbon dioxide gas-sensitive electrode.|10. A computer-readable storage medium characterized by: the computer-readable storage medium stores a computer program which, when executed by one or more processors, is capable of implementing the method for carbon sink capacity assessment based on watershed scale karstic weathering as claimed in any one of claims 1 to 6. (CN115728223)|TECHNICAL FIELD|[0001] The invention relates to the technical field of carbon sink monitoring, in particular to a method, a device, a system and a medium for evaluating carbon sink capacity based on drainage basin scale karst weathering.|BACKGROUND ART|[0002] The 'carbon peak reaching and carbon neutralization' target is an important content of ecological civilization construction, and carbon sink is also greatly increased in addition to large-scale emission reduction to realize the carbon neutralization target. At present, carbon sink comprises plant carbon sink, soil carbon sink, ocean carbon sink, geological carbon sink and the like, wherein the karst carbon sink is a main component of the geological carbon sink, and China is used as a karst big country, the distribution area occupies about 1/6 of the world, and can make significant contribution to global carbon neutralization, so that the method is particularly important for evaluating the capability of the karst carbon sink.|[0003] The karst carbon sink refers to the carbon sink effect generated in the karst action process, the karst action is the corrosion weathering process of water to soluble rock, and the chemical equation isIt is a dynamic equilibrium system, i.e. 1mol of Ca is dissolved away x Mg (1-x) CO 3 Can absorb 1mol of CO from the atmosphere or soil 2 And 2mol of HCO was formed 3- At the fluid field scale, HCO 3- It is transferred into the water body. Based on the method, the HCO in the water body is treated 3- The source of (A) is analyzed and reasonably adopted, and CO can be calculated 2 Consumption and corresponding carbon sink strength, but the existing monitoring mainly comprises manual sampling and laboratory analysis, and scientific and efficient monitoring technical means are lacked to support research on evaluation of karst carbon sink capacity.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to solve the problems and designs a carbon sink capacity evaluation method, a device, a system and a medium based on basin scale karst weathering, which can effectively improve the accuracy and the practicability of carbon sink capacity evaluation.|[0005] In order to achieve the purpose, the technical scheme of the invention is as follows:|[0006] a carbon sink capacity evaluation method based on watershed scale karst weathering comprises the following steps:|[0007] s1, selecting a monitoring section: selecting an outlet section of the drainage basin as a monitoring section, wherein the drainage basin comprises: rivers with a defined watershed range and rivers without a defined watershed range;|[0008] s2, acquiring real-time hydrological information: the hydrologic information includes: the cross section area, the cross section flow, the water flow velocity, the water surface elevation and the water flow direction;|[0009] s3, acquiring real-time water quality information: the water quality information comprises: pH value, water temperature, HCO 3- Concentration;|[0010] s4, calculating CO 2 Consumption flux: combining hydrological information and water quality information and calculating CO by using an integral mode 2 Consuming the flux;|[0011] s5, calculating the carbon sink strength: binding of CO 2 The carbon sink strength was calculated from the flux consumed and the basin area.|[0012] Further, S1 further includes: and selecting a drainage basin outlet section which is superposed with the existing hydrological station or automatic water quality monitoring station as a monitoring section.|[0013] Further, S2 further includes: acquiring the hydrological information by selecting any one of an acoustic Doppler principle, an ultrasonic time difference method and a radar wave principle;|[0014] s3 further comprises: HCO calculation by ion selective electrode method 3- Concentration, the formula is as follows:|[0015] |[0016] wherein, K 1 、K 2 Is a constant number, C T Is water temperature, [ H ] + ]Represents H + The ion concentration.|[0017] Further, S3 further includes: and monitoring points for acquiring water quality information are uniformly distributed along the outlet section of the basin.|[0018] Further, S4 further includes:|[0019] CO 2 the formula for the consumed flux is as follows:|[0020] W=∫ T F(t)dt=∫ T Q(t)C(t)dt=Q a C a T+∫ T Q"C"d|[0021] F=W x 44/(2 x 61)|[0022] wherein W is HCO 3- Ion flux (g/s), Q a Is the time interval average flow (m) 3 /s),C a Is a period of HCO 3- Average concentration (mg/L), T is an estimation time period, Q 'is a flow time average distance average value, and C' is a concentration time average distance average value; f is CO 2 Flux (g/s) was consumed.|[0023] Further, S5 further includes:|[0024] the carbon sink strength is calculated as follows:|[0025] I=F/K|[0026] wherein I is the basin carbon sink strength (t/km) 2 A); f is CO 2 Consumption flux (t/a); k is the basin area (km) 2 )。|[0027] A carbon sink capacity evaluation device based on watershed scale karst weathering comprises the following modules:|[0028] the drainage basin dividing module is used for extracting a river network and demarcating water catchment units based on digital elevation model data by adopting a GIS technology to complete drainage basin division;|[0029] the monitoring section setting module is used for fusing the distribution conditions of the existing automatic water quality monitoring stations and hydrological stations and automatically screening the monitoring sections;|[0030] the data acquisition module is used for acquiring hydrological information and water quality information, the hydrological information comprises but is not limited to section area, section flow, water flow velocity, water surface elevation and water flow direction, and the water quality information comprises but is not limited to pH value, water temperature and HCO 3- Concentration;|[0031] the data processing module is used for matching effective hydrological information and water quality information data, deleting redundant and abnormal data and calculating HCO 3- Ion flux, CO 2 Consuming the flux;|[0032] and the evaluation module generates a karst carbon sink strength report of the watershed scale.|[0033] A carbon sink capacity evaluation system based on drainage basin scale karst weathering comprises a main control unit, an acquisition unit, a storage unit, a communication unit and a power supply unit;|[0034] the storage unit is used for storing a computer program;|[0035] the main control unit comprises a processor, and when the processor executes the computer program, the carbon sink capacity evaluation method based on the watershed scale karst weathering can be realized;|[0036] the acquisition unit comprises a hydrological monitor for acquiring hydrological information and a water quality monitor for acquiring water quality information, and the hydrological monitor and the water quality monitor are in data communication with the processor;|[0037] the communication unit is used for realizing data communication between the processor and the background;|[0038] the power supply unit is used for supplying power to each functional unit.|[0039] Furthermore, the hydrological monitor is an acoustic Doppler current meter which is connected with a plurality of ultrasonic probes;|[0040] the water quality monitor adopts a multi-channel ion potentiometer which is connected with a pH electrode and a carbon dioxide gas-sensitive electrode.|[0041] A computer readable storage medium storing a computer program which, when executed by one or more processors, is capable of implementing the carbon sink capacity assessment method based on watershed scale karstic weathering as described in any one of the preceding claims.|[0042] Compared with the prior art, the invention has the advantages and positive effects that: the invention creatively provides a carbon sink capacity evaluation method, device, system and medium based on watershed scale karst weathering, and provides a new research direction for dynamic monitoring and quantitative calculation in the karst carbon sink weathering process. The hydrological information data and the water quality information data can be continuously collected and processed in real time to obtain synchronous and high-resolution data, and timeliness and accuracy of carbon sink capacity evaluation can be effectively guaranteed. In addition, the monitoring sections are selected by combining the distribution conditions of the existing automatic water quality monitoring stations, hydrological stations and the like, and the cost for selecting the monitoring sections can be saved on the basis of ensuring the accuracy of carbon sink capacity evaluation.|DRAWINGS DESCRIPTION|[0043] In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings required to be used in the embodiments or the prior art description will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings may be obtained according to these drawings without inventive labor.|[0044] Fig. 1 is a schematic flow chart of a carbon sequestration capacity evaluation method based on watershed scale karst weathering according to the present invention;|[0045] fig. 2 is a schematic block diagram of a carbon sequestration capacity evaluation device based on watershed scale karst weathering according to the present invention;|[0046] fig. 3 is a schematic diagram of a framework of a system for evaluating carbon sequestration capacity based on watershed scale karst weathering according to the present invention;|[0047] fig. 4 is a block diagram of a computer-readable storage medium according to the present invention.|INVENTION MODE|Detailed Description|[0048] Embodiments of the present invention will be described in detail below with reference to the accompanying drawings. The following examples are only for illustrating the technical solutions of the present invention more clearly, and therefore are only used as examples, and the protection scope of the present invention is not limited thereby.|[0049] It is to be noted that unless otherwise specified, technical or scientific terms used herein shall be taken as the ordinary meaning as understood by those skilled in the art to which the invention pertains.|[0050] Provided are a carbon sink capacity evaluation method, system, medium and equipment based on watershed scale karst weathering. Embodiments of the present invention will be described below with reference to the drawings.|[0051] The first embodiment:|[0052] as shown in fig. 1, this embodiment provides a carbon sequestration capacity evaluation method based on watershed scale karst weathering, including the following steps:|[0053] s1, selecting a monitoring section: selecting an outlet section of the drainage basin as a monitoring section, wherein the drainage basin comprises: a river with a watershed defined and a river without a watershed defined;|[0054] s2, acquiring real-time hydrological information: the hydrologic information includes: the cross section area, the cross section flow, the water flow velocity, the water surface elevation and the water flow direction;|[0055] s3, acquiring real-time water quality information: the water quality information comprises: pH value, water temperature, HCO 3- Concentration;|[0056] s4, calculating CO 2 Consumption flux: the hydrological information and the water quality information are combined, and the CO is calculated by utilizing an integral mode 2 Consuming the flux;|[0057] s5, calculating the carbon sink strength: binding to CO 2 The carbon sink strength was calculated from the consumed flux and the basin area.|[0058] The watershed may be a river having a watershed area defined therein, or a river having a watershed area not defined therein. The control unit and the watershed range are defined by adopting a GIS technology, determining the land range according to the catchment relation based on Digital Elevation Model (DEM) data and forming a land and water combination unit, including river network extraction, automatic watershed division and the like.|[0059] In addition, a drainage basin with small influence on human activities, namely SO, should be selected as a monitoring object 2 And NO 2 The watershed with less pollution can pass through the air station SO in the watershed or around 2 And NO 2 Whether the 24-hour average concentration value is lower than the secondary standard of the environmental air quality standard (GB 3095-2012) is judged quantitatively. Meanwhile, the characteristic ion determination of 1 month can be carried out in advance, and particularly, ca of the monitored section can be determined 2+ 、Mg 2+ 、HCO 3- Plasma sampling and laboratory analysis and determination (ion chromatography optionally) in water (Ca) 2+ +Mg 2+ ) With HCO 3- When the equivalent ratio of (A) is 1. + -. 0.05, the method described in the present example is used, and if it exceeds the above range, the present example is not applied, and the influence of an exogenous acid such as sulfuric acid or nitric acid is not necessary to be additionally reduced.|[0060] When the monitoring section is selected, the river channel is straight, the water flow is smooth and the river bed is regular within the range of 2km of the drainage basin outlet, so that the monitored data are more stable and accurate.|[0061] Preferably, S1 further comprises: and selecting a watershed outlet section which is superposed with the existing hydrological station or the automatic water quality monitoring station as a monitoring section.|[0062] In this embodiment, the selection cost of the monitoring section can be saved on the basis of ensuring the monitoring accuracy by the operation. Specifically, when the real-time hydrologic site coincides with the hydrologic site, the real-time hydrologic information is acquired through the hydrologic site; when the water quality monitoring station coincides with the automatic water quality monitoring station, the real-time water quality information is obtained through the automatic water quality monitoring station.|[0063] Preferably, S2 further comprises: acquiring the hydrological information by selecting any one of an acoustic Doppler principle, an ultrasonic time difference method and a radar wave principle;|[0064] s3, further comprising: HCO calculation by ion selective electrode method 3- Concentration, the formula is as follows:|[0065] |[0066] wherein, K 1 、K 2 Is a constant number, C T Water temperature, [ H ] + ]Is represented by H + The ion concentration.|[0067] Preferably, S3 further comprises: and monitoring points for acquiring water quality information are uniformly distributed along the outlet section of the basin.|[0068] In the embodiment, a plurality of water quality monitoring points are distributed at equal intervals according to the condition of the section in a certain quantity at the left side, the middle side and the right side of the section.|[0069] Preferably, S4 further comprises:|[0070] CO 2 the calculation formula of the consumed flux is as follows:|[0071] W=∫ T F(t)dt=∫ T Q(t)C(t)dt=Q a C a T+∫ T Q″C"d|[0072] F=W x 44/(2 x 61)|[0073] wherein W is HCO 3 Ion flux (g/s), Q a Is the time interval average flow (m) 3 /s),C a Is a period of HCO 3- Average concentration (mg/L), T is estimation time interval, Q 'is average distance average value in flow, and C' is average distance average value in concentration; f is CO 2 Flux (g/s) was consumed.|[0074] Preferably, S5 further comprises:|[0075] the formula for calculating the carbon sink strength is as follows:|[0076] I=F/K|[0077] wherein I is the basin carbon sink strength (t/km) 2 A); f is CO 2 Consumption flux (t/a); k is the basin area (km) 2 )。|[0078] The second embodiment:|[0079] as shown in fig. 3, a system for evaluating carbon sink capacity based on watershed scale karst weathering includes a main control unit 21, an acquisition unit 22, a storage unit 23, a communication unit 24, and a power supply unit 25;|[0080] the storage unit is used for storing a computer program;|[0081] the main control unit comprises a processor, and when the processor executes the computer program, the carbon sink capacity evaluation method based on the watershed scale karst weathering, as described in any one of the first embodiments, can be realized;|[0082] the acquisition unit comprises a hydrological monitor for acquiring hydrological information and a water quality monitor for acquiring water quality information, and the hydrological monitor and the water quality monitor are in data communication with the processor;|[0083] the communication unit is used for realizing data communication between the processor and the background;|[0084] the power supply unit is used for supplying power to each functional unit.|[0085] Preferably, the hydrological monitor is an acoustic Doppler current meter which is connected with a plurality of ultrasonic probes;|[0086] the water quality monitor adopts a multi-channel ion potentiometer which is connected with a pH electrode and a carbon dioxide gas-sensitive electrode.|[0087] In this embodiment, the processor may be a single chip microcomputer. A keyboard and a display screen can be arranged for facilitating the instruction input and the viewing. An operator can transmit an instruction to the processor in a keyboard input mode, so that the corresponding hydrological monitor and the corresponding water quality monitor are in an online monitoring state.|[0088] The processor can also adopt an ARM framework all-in-one machine which is integrated with a TFT display screen and a touch screen.|[0089] The communication unit CAN select a wired communication module, such as a CAN communication module and an Ethernet module, and the communication unit CAN also select a wireless communication module, such as a WIFI module. The processor can transmit data to the background through the communication unit.|[0090] The background can be a mobile terminal or a PC terminal, and can also be a cloud server.|[0091] The power supply unit should include each power conversion module, such as a 220V to 12V step-down module, a 12V to 5V step-down module, and a 5V to 3.3V step-down module, or a 220V to 24V step-down module, a 24V to 12V step-down module, a 12V to 5V step-down module, and a 5V to 3.3V step-down module, so as to supply power to each functional unit.|[0092] The data communication means between the hydrological monitor and the water quality monitor and the processor can be through an RS232 interface, and the acoustic Doppler current meter can be through ultrasonicThe wave probe monitors the flow of the cross section and the flow velocity of water flow, and the multichannel ion potentiometer can measure HCO of water body at the cross section through the carbon dioxide gas-sensitive electrode and the pH electrode 3- Concentration, voltage, water temperature.|[0093] The storage unit may be an internal storage unit, such as a memory, or an external storage device, such as a plug-in hard disk.|[0094] Preferably, the collection unit further comprises a means for measuring Ca 2+ Calcium ion selective electrode and method for measuring Mg 2+ The calcium ion selective electrode and the spectrophotometer are connected with the processor when the water (Ca) is in the water 2+ +Mg 2+ ) With HCO 3- When the equivalent ratio is 1 +/-0.05, the operation of the carbon sink capacity evaluation method can be continued, otherwise, a corresponding prompt report is generated. Of course, the operator may input real-time ion measurement data to communicate instructions to the processor.|[0095] S1, selecting a monitoring section|[0096] Taking the river generally river within the defined watershed as an example,|[0097] the length of the Puzi river is 66km, and the area of the river basin is 801km 2 Average flow rate of 22.0m for many years 3 And/s, injecting Yujiang at the mouth of the three rivers. There is no hydrology site or automatic water quality monitoring site, and the section is set in the flat and straight river section with smooth water flow.|[0098] HCO of river water upstream of cross section 3- Mainly from the effects of carbonate weathering and silicate weathering, and less influence of human activity, in the body of water (Ca) 2+ +Mg 2+ ) With HCO 3- The equivalent ratio of (A) is 1-1.02, and the method is an ideal area for analyzing the consumption flux of the drainage basin mineral weathering process to the atmospheric CO 2.|[0099] S2, acquiring real-time hydrological information|[0100] The cross section of the three river mouths of the ordinary river has the width of 30-40m and the depth of water of 2-5m, is a wide and shallow river channel, and adopts an acoustic Doppler flow velocity method to measure hydrological information such as flow, flow velocity and the like. The working principle of the ultrasonic flow meter is that a probe is fixedly arranged at a certain water depth under the water surface, two acoustic sensors on the probe are positioned on the same plane, two ultrasonic sensors are emitted to the opposite bank at a certain angle, the frequency of ultrasonic waves is changed when the ultrasonic waves meet bubble impurities and the like in water, and the two-dimensional flow rate of each point on a certain section of the water flow of the layer is calculated according to the frequency; and the other beam of ultrasonic wave is emitted upwards and meets the water surface to reflect and measure the water depth. And obtaining the average flow velocity of the cross section according to a pre-established mathematical model, and calculating the flow value according to the actual flow area of the river channel.|[0101] S3, acquiring real-time water quality information|[0102] Carbon dioxide gas-sensitive electrodes of a multi-channel ion potentiometer are arranged at the left, middle and right three points of the monitored section, and the water temperature and HCO of each point on the section are monitored in real time through the Nernst equation and the carbonic acid balance principle 3- And (4) concentration. The left and right points are respectively arranged at 1m-2m off-shore with obvious water flow, and the middle point can be arranged on a Chinese body line.|[0103] In addition, during this period, the operator analyzed Ca on the monitored section by ion electrode or laboratory in a manner of 1 time/month 2+ 、Mg 2+ 、HCO 3- And (3) measuring, wherein the monitoring points are the same as the hydrological water quality monitoring points, and the result is as follows: in water (Ca) 2+ +Mg 2+ ) With HCO 3- The equivalent ratio of (a) to (b) is between 1 and 1.05, the evaluation can be continued using this example.|[0104] S4, calculating CO 2 Consuming flux|[0105] The data obtained in the steps S2 and S3 are integrated according to the monthly time period to obtain the monthly mean flow and HCO 3- And (4) concentration, and further obtaining the monthly karst weathering CO2 consumption flux of the Puzi river basin, which is shown in the table below. Karst weathering CO of Puzi river basin 2 The consumed flux was 80717.95t/a.|[0106] |[0107] |[0108] S5, calculating the carbon sink strength|[0109] And substituting the karst CO2 consumption flux 80717.95 (t/a) and the area 801km2 of the basin into a basin carbon sink strength calculation formula to calculate the basin carbon sink strength 100.8 (t/km2. A).|[0110] The third embodiment:|[0111] as shown in fig. 2, a carbon sequestration capacity assessment device based on watershed scale karst weathering is characterized in that: the method comprises the following steps:|[0112] the drainage basin dividing module 11 is used for extracting a river network and dividing water catchment units based on digital elevation model data by adopting a GIS technology to finish drainage basin division;|[0113] the monitoring section setting module 12 is used for integrating the distribution conditions of the existing automatic water quality monitoring stations and hydrological stations and automatically screening monitoring sections;|[0114] the data acquisition module 13 comprises acquisition hydrological information 131 and acquisition water quality information 132, wherein the hydrological information includes but is not limited to section area, section flow, water flow rate, water surface elevation and water flow direction, and the water quality information includes but is not limited to pH value and water temperature;|[0115] the data processing module 14 is used for matching effective hydrological information and water quality information data, deleting redundant and abnormal data and calculating HCO 3- Concentration, CO2 consumption flux;|[0116] and the evaluation module 15 generates a karst carbon sink strength report of the watershed scale.|[0117] In this embodiment, when selecting specific basin, then can divide according to the basin and select corresponding monitoring section automatically to can read the data that hydrology monitor and the water quality monitoring appearance that correspond on the monitoring section gathered through data acquisition module. The data processing module can process data according to an input instruction of an operator, and the matched effective data is ready for calculation. In the evaluation module, CO is generated according to information such as hydrology, water quality and the like 2 Consumption flux, watershed carbon sink strength evaluation report.|[0118] Preferably, in the drainage basin dividing module 11, a drainage basin with small human activity influence should be selected as a monitoring object, that is, SO 2 、NO 2 And the like, less contaminated watersheds. Ion electrode and laboratory analysis can be selected in advance for Ca in water 2+ 、Mg 2+ 、HCO 3- Plasma measurement of (Ca) in water 2+ +Mg 2+ ) With HCO 3- Should be 1. + -. 0.05. Otherwise the present evaluation device is not applicable.|[0119] Preferably, in the monitoring section setting module 12, a drainage basin outlet section which is overlapped with an existing hydrological station or an existing automatic water quality monitoring station can be selected as a monitoring section; if no corresponding station exists, the position with straight river channel, smooth water flow and regular river bed within the range of 2km at the drainage basin outlet can be selected.|[0120] Preferably, in the data acquisition module 13, ca in the water body should be acquired 2+ 、Mg 2+ 、HCO 3- To calculate (Ca) in the water body 2+ +Mg 2+ ) With HCO 3- The equivalent ratio of (a).|[0121] Preferably, in the data processing module 14, the (Ca) in the water body is detected 2+ +Mg 2+ ) With HCO 3- Whether the equivalent ratio of (A) is within 1 + -0.05, and generating a corresponding prompt report to verify HCO 3- The effectiveness of (c).|[0122] The fourth embodiment:|[0123] as shown in fig. 4, a computer-readable storage medium 31 stores a computer program, which when executed by one or more processors can implement the carbon sequestration capacity assessment method based on basin scale karstic weathering as described in any one of the first embodiments.|[0124] In this embodiment, the computer program may be divided into one or more modules, and these modules may be a series of computer program instruction segments capable of performing specific functions as described in the first embodiment and the third embodiment, and the instruction segments are used for describing the processes executed by the computer program. The storage medium may be a magnetic disk storage and an optical storage.|[0125] The foregoing is a more detailed description of the present invention in connection with specific preferred embodiments thereof, and it is not intended that the specific embodiments of the present invention be limited to these descriptions. Other embodiments that can be derived by a person skilled in the art without departing from the scope of the present invention are also intended to be included within the scope of the present invention. (CN115728223)|TECHNICAL FIELD|[0001] The invention relates to the technical field of carbon sink monitoring, in particular to a method, a device, a system and a medium for evaluating carbon sink capacity based on drainage basin scale karst weathering.|BACKGROUND ART|[0002] The 'carbon peak reaching and carbon neutralization' target is an important content of ecological civilization construction, and carbon sink is also greatly increased in addition to large-scale emission reduction to realize the carbon neutralization target. At present, carbon sink comprises plant carbon sink, soil carbon sink, ocean carbon sink, geological carbon sink and the like, wherein the karst carbon sink is a main component of the geological carbon sink, and China is used as a karst big country, the distribution area occupies about 1/6 of the world, and can make significant contribution to global carbon neutralization, so that the method is particularly important for evaluating the capability of the karst carbon sink.|[0003] The karst carbon sink refers to the carbon sink effect generated in the karst action process, the karst action is the corrosion weathering process of water to soluble rock, and the chemical equation isIt is a dynamic equilibrium system, i.e. 1mol of Ca is dissolved away x Mg (1-x) CO 3 Can absorb 1mol of CO from the atmosphere or soil 2 And 2mol of HCO was formed 3- At the fluid field scale, HCO 3- It is transferred into the water body. Based on the method, the HCO in the water body is treated 3- The source of (A) is analyzed and reasonably adopted, and CO can be calculated 2 Consumption and corresponding carbon sink strength, but the existing monitoring mainly comprises manual sampling and laboratory analysis, and scientific and efficient monitoring technical means are lacked to support research on evaluation of karst carbon sink capacity.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to solve the problems and designs a carbon sink capacity evaluation method, a device, a system and a medium based on basin scale karst weathering, which can effectively improve the accuracy and the practicability of carbon sink capacity evaluation.|[0005] In order to achieve the purpose, the technical scheme of the invention is as follows:|[0006] a carbon sink capacity evaluation method based on watershed scale karst weathering comprises the following steps:|[0007] s1, selecting a monitoring section: selecting an outlet section of the drainage basin as a monitoring section, wherein the drainage basin comprises: rivers with a defined watershed range and rivers without a defined watershed range;|[0008] s2, acquiring real-time hydrological information: the hydrologic information includes: the cross section area, the cross section flow, the water flow velocity, the water surface elevation and the water flow direction;|[0009] s3, acquiring real-time water quality information: the water quality information comprises: pH value, water temperature, HCO 3- Concentration;|[0010] s4, calculating CO 2 Consumption flux: combining hydrological information and water quality information and calculating CO by using an integral mode 2 Consuming the flux;|[0011] s5, calculating the carbon sink strength: binding of CO 2 The carbon sink strength was calculated from the flux consumed and the basin area.|[0012] Further, S1 further includes: and selecting a drainage basin outlet section which is superposed with the existing hydrological station or automatic water quality monitoring station as a monitoring section.|[0013] Further, S2 further includes: acquiring the hydrological information by selecting any one of an acoustic Doppler principle, an ultrasonic time difference method and a radar wave principle;|[0014] s3 further comprises: HCO calculation by ion selective electrode method 3- Concentration, the formula is as follows:|[0015] |[0016] wherein, K 1 、K 2 Is a constant number, C T Is water temperature, [ H ] + ]Represents H + The ion concentration.|[0017] Further, S3 further includes: and monitoring points for acquiring water quality information are uniformly distributed along the outlet section of the basin.|[0018] Further, S4 further includes:|[0019] CO 2 the formula for the consumed flux is as follows:|[0020] W=∫ T F(t)dt=∫ T Q(t)C(t)dt=Q a C a T+∫ T Q"C"d|[0021] F=W x 44/(2 x 61)|[0022] wherein W is HCO 3- Ion flux (g/s), Q a Is the time interval average flow (m) 3 /s),C a Is a period of HCO 3- Average concentration (mg/L), T is an estimation time period, Q 'is a flow time average distance average value, and C' is a concentration time average distance average value; f is CO 2 Flux (g/s) was consumed.|[0023] Further, S5 further includes:|[0024] the carbon sink strength is calculated as follows:|[0025] I=F/K|[0026] wherein I is the basin carbon sink strength (t/km) 2 A); f is CO 2 Consumption flux (t/a); k is the basin area (km) 2 )。|[0027] A carbon sink capacity evaluation device based on watershed scale karst weathering comprises the following modules:|[0028] the drainage basin dividing module is used for extracting a river network and demarcating water catchment units based on digital elevation model data by adopting a GIS technology to complete drainage basin division;|[0029] the monitoring section setting module is used for fusing the distribution conditions of the existing automatic water quality monitoring stations and hydrological stations and automatically screening the monitoring sections;|[0030] the data acquisition module is used for acquiring hydrological information and water quality information, the hydrological information comprises but is not limited to section area, section flow, water flow velocity, water surface elevation and water flow direction, and the water quality information comprises but is not limited to pH value, water temperature and HCO 3- Concentration;|[0031] the data processing module is used for matching effective hydrological information and water quality information data, deleting redundant and abnormal data and calculating HCO 3- Ion flux, CO 2 Consuming the flux;|[0032] and the evaluation module generates a karst carbon sink strength report of the watershed scale.|[0033] A carbon sink capacity evaluation system based on drainage basin scale karst weathering comprises a main control unit, an acquisition unit, a storage unit, a communication unit and a power supply unit;|[0034] the storage unit is used for storing a computer program;|[0035] the main control unit comprises a processor, and when the processor executes the computer program, the carbon sink capacity evaluation method based on the watershed scale karst weathering can be realized;|[0036] the acquisition unit comprises a hydrological monitor for acquiring hydrological information and a water quality monitor for acquiring water quality information, and the hydrological monitor and the water quality monitor are in data communication with the processor;|[0037] the communication unit is used for realizing data communication between the processor and the background;|[0038] the power supply unit is used for supplying power to each functional unit.|[0039] Furthermore, the hydrological monitor is an acoustic Doppler current meter which is connected with a plurality of ultrasonic probes;|[0040] the water quality monitor adopts a multi-channel ion potentiometer which is connected with a pH electrode and a carbon dioxide gas-sensitive electrode.|[0041] A computer readable storage medium storing a computer program which, when executed by one or more processors, is capable of implementing the carbon sink capacity assessment method based on watershed scale karstic weathering as described in any one of the preceding claims.|[0042] Compared with the prior art, the invention has the advantages and positive effects that: the invention creatively provides a carbon sink capacity evaluation method, device, system and medium based on watershed scale karst weathering, and provides a new research direction for dynamic monitoring and quantitative calculation in the karst carbon sink weathering process. The hydrological information data and the water quality information data can be continuously collected and processed in real time to obtain synchronous and high-resolution data, and timeliness and accuracy of carbon sink capacity evaluation can be effectively guaranteed. In addition, the monitoring sections are selected by combining the distribution conditions of the existing automatic water quality monitoring stations, hydrological stations and the like, and the cost for selecting the monitoring sections can be saved on the basis of ensuring the accuracy of carbon sink capacity evaluation.|DRAWINGS DESCRIPTION|[0043] In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings required to be used in the embodiments or the prior art description will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings may be obtained according to these drawings without inventive labor.|[0044] Fig. 1 is a schematic flow chart of a carbon sequestration capacity evaluation method based on watershed scale karst weathering according to the present invention;|[0045] fig. 2 is a schematic block diagram of a carbon sequestration capacity evaluation device based on watershed scale karst weathering according to the present invention;|[0046] fig. 3 is a schematic diagram of a framework of a system for evaluating carbon sequestration capacity based on watershed scale karst weathering according to the present invention;|[0047] fig. 4 is a block diagram of a computer-readable storage medium according to the present invention.|INVENTION MODE|Detailed Description|[0048] Embodiments of the present invention will be described in detail below with reference to the accompanying drawings. The following examples are only for illustrating the technical solutions of the present invention more clearly, and therefore are only used as examples, and the protection scope of the present invention is not limited thereby.|[0049] It is to be noted that unless otherwise specified, technical or scientific terms used herein shall be taken as the ordinary meaning as understood by those skilled in the art to which the invention pertains.|[0050] Provided are a carbon sink capacity evaluation method, system, medium and equipment based on watershed scale karst weathering. Embodiments of the present invention will be described below with reference to the drawings.|[0051] The first embodiment:|[0052] as shown in fig. 1, this embodiment provides a carbon sequestration capacity evaluation method based on watershed scale karst weathering, including the following steps:|[0053] s1, selecting a monitoring section: selecting an outlet section of the drainage basin as a monitoring section, wherein the drainage basin comprises: a river with a watershed defined and a river without a watershed defined;|[0054] s2, acquiring real-time hydrological information: the hydrologic information includes: the cross section area, the cross section flow, the water flow velocity, the water surface elevation and the water flow direction;|[0055] s3, acquiring real-time water quality information: the water quality information comprises: pH value, water temperature, HCO 3- Concentration;|[0056] s4, calculating CO 2 Consumption flux: the hydrological information and the water quality information are combined, and the CO is calculated by utilizing an integral mode 2 Consuming the flux;|[0057] s5, calculating the carbon sink strength: binding to CO 2 The carbon sink strength was calculated from the consumed flux and the basin area.|[0058] The watershed may be a river having a watershed area defined therein, or a river having a watershed area not defined therein. The control unit and the watershed range are defined by adopting a GIS technology, determining the land range according to the catchment relation based on Digital Elevation Model (DEM) data and forming a land and water combination unit, including river network extraction, automatic watershed division and the like.|[0059] In addition, a drainage basin with small influence on human activities, namely SO, should be selected as a monitoring object 2 And NO 2 The watershed with less pollution can pass through the air station SO in the watershed or around 2 And NO 2 Whether the 24-hour average concentration value is lower than the secondary standard of the environmental air quality standard (GB 3095-2012) is judged quantitatively. Meanwhile, the characteristic ion determination of 1 month can be carried out in advance, and particularly, ca of the monitored section can be determined 2+ 、Mg 2+ 、HCO 3- Plasma sampling and laboratory analysis and determination (ion chromatography optionally) in water (Ca) 2+ +Mg 2+ ) With HCO 3- When the equivalent ratio of (A) is 1. + -. 0.05, the method described in the present example is used, and if it exceeds the above range, the present example is not applied, and the influence of an exogenous acid such as sulfuric acid or nitric acid is not necessary to be additionally reduced.|[0060] When the monitoring section is selected, the river channel is straight, the water flow is smooth and the river bed is regular within the range of 2km of the drainage basin outlet, so that the monitored data are more stable and accurate.|[0061] Preferably, S1 further comprises: and selecting a watershed outlet section which is superposed with the existing hydrological station or the automatic water quality monitoring station as a monitoring section.|[0062] In this embodiment, the selection cost of the monitoring section can be saved on the basis of ensuring the monitoring accuracy by the operation. Specifically, when the real-time hydrologic site coincides with the hydrologic site, the real-time hydrologic information is acquired through the hydrologic site; when the water quality monitoring station coincides with the automatic water quality monitoring station, the real-time water quality information is obtained through the automatic water quality monitoring station.|[0063] Preferably, S2 further comprises: acquiring the hydrological information by selecting any one of an acoustic Doppler principle, an ultrasonic time difference method and a radar wave principle;|[0064] s3, further comprising: HCO calculation by ion selective electrode method 3- Concentration, the formula is as follows:|[0065] |[0066] wherein, K 1 、K 2 Is a constant number, C T Water temperature, [ H ] + ]Is represented by H + The ion concentration.|[0067] Preferably, S3 further comprises: and monitoring points for acquiring water quality information are uniformly distributed along the outlet section of the basin.|[0068] In the embodiment, a plurality of water quality monitoring points are distributed at equal intervals according to the condition of the section in a certain quantity at the left side, the middle side and the right side of the section.|[0069] Preferably, S4 further comprises:|[0070] CO 2 the calculation formula of the consumed flux is as follows:|[0071] W=∫ T F(t)dt=∫ T Q(t)C(t)dt=Q a C a T+∫ T Q″C"d|[0072] F=W x 44/(2 x 61)|[0073] wherein W is HCO 3 Ion flux (g/s), Q a Is the time interval average flow (m) 3 /s),C a Is a period of HCO 3- Average concentration (mg/L), T is estimation time interval, Q 'is average distance average value in flow, and C' is average distance average value in concentration; f is CO 2 Flux (g/s) was consumed.|[0074] Preferably, S5 further comprises:|[0075] the formula for calculating the carbon sink strength is as follows:|[0076] I=F/K|[0077] wherein I is the basin carbon sink strength (t/km) 2 A); f is CO 2 Consumption flux (t/a); k is the basin area (km) 2 )。|[0078] The second embodiment:|[0079] as shown in fig. 3, a system for evaluating carbon sink capacity based on watershed scale karst weathering includes a main control unit 21, an acquisition unit 22, a storage unit 23, a communication unit 24, and a power supply unit 25;|[0080] the storage unit is used for storing a computer program;|[0081] the main control unit comprises a processor, and when the processor executes the computer program, the carbon sink capacity evaluation method based on the watershed scale karst weathering, as described in any one of the first embodiments, can be realized;|[0082] the acquisition unit comprises a hydrological monitor for acquiring hydrological information and a water quality monitor for acquiring water quality information, and the hydrological monitor and the water quality monitor are in data communication with the processor;|[0083] the communication unit is used for realizing data communication between the processor and the background;|[0084] the power supply unit is used for supplying power to each functional unit.|[0085] Preferably, the hydrological monitor is an acoustic Doppler current meter which is connected with a plurality of ultrasonic probes;|[0086] the water quality monitor adopts a multi-channel ion potentiometer which is connected with a pH electrode and a carbon dioxide gas-sensitive electrode.|[0087] In this embodiment, the processor may be a single chip microcomputer. A keyboard and a display screen can be arranged for facilitating the instruction input and the viewing. An operator can transmit an instruction to the processor in a keyboard input mode, so that the corresponding hydrological monitor and the corresponding water quality monitor are in an online monitoring state.|[0088] The processor can also adopt an ARM framework all-in-one machine which is integrated with a TFT display screen and a touch screen.|[0089] The communication unit CAN select a wired communication module, such as a CAN communication module and an Ethernet module, and the communication unit CAN also select a wireless communication module, such as a WIFI module. The processor can transmit data to the background through the communication unit.|[0090] The background can be a mobile terminal or a PC terminal, and can also be a cloud server.|[0091] The power supply unit should include each power conversion module, such as a 220V to 12V step-down module, a 12V to 5V step-down module, and a 5V to 3.3V step-down module, or a 220V to 24V step-down module, a 24V to 12V step-down module, a 12V to 5V step-down module, and a 5V to 3.3V step-down module, so as to supply power to each functional unit.|[0092] The data communication means between the hydrological monitor and the water quality monitor and the processor can be through an RS232 interface, and the acoustic Doppler current meter can be through ultrasonicThe wave probe monitors the flow of the cross section and the flow velocity of water flow, and the multichannel ion potentiometer can measure HCO of water body at the cross section through the carbon dioxide gas-sensitive electrode and the pH electrode 3- Concentration, voltage, water temperature.|[0093] The storage unit may be an internal storage unit, such as a memory, or an external storage device, such as a plug-in hard disk.|[0094] Preferably, the collection unit further comprises a means for measuring Ca 2+ Calcium ion selective electrode and method for measuring Mg 2+ The calcium ion selective electrode and the spectrophotometer are connected with the processor when the water (Ca) is in the water 2+ +Mg 2+ ) With HCO 3- When the equivalent ratio is 1 +/-0.05, the operation of the carbon sink capacity evaluation method can be continued, otherwise, a corresponding prompt report is generated. Of course, the operator may input real-time ion measurement data to communicate instructions to the processor.|[0095] S1, selecting a monitoring section|[0096] Taking the river generally river within the defined watershed as an example,|[0097] the length of the Puzi river is 66km, and the area of the river basin is 801km 2 Average flow rate of 22.0m for many years 3 And/s, injecting Yujiang at the mouth of the three rivers. There is no hydrology site or automatic water quality monitoring site, and the section is set in the flat and straight river section with smooth water flow.|[0098] HCO of river water upstream of cross section 3- Mainly from the effects of carbonate weathering and silicate weathering, and less influence of human activity, in the body of water (Ca) 2+ +Mg 2+ ) With HCO 3- The equivalent ratio of (A) is 1-1.02, and the method is an ideal area for analyzing the consumption flux of the drainage basin mineral weathering process to the atmospheric CO 2.|[0099] S2, acquiring real-time hydrological information|[0100] The cross section of the three river mouths of the ordinary river has the width of 30-40m and the depth of water of 2-5m, is a wide and shallow river channel, and adopts an acoustic Doppler flow velocity method to measure hydrological information such as flow, flow velocity and the like. The working principle of the ultrasonic flow meter is that a probe is fixedly arranged at a certain water depth under the water surface, two acoustic sensors on the probe are positioned on the same plane, two ultrasonic sensors are emitted to the opposite bank at a certain angle, the frequency of ultrasonic waves is changed when the ultrasonic waves meet bubble impurities and the like in water, and the two-dimensional flow rate of each point on a certain section of the water flow of the layer is calculated according to the frequency; and the other beam of ultrasonic wave is emitted upwards and meets the water surface to reflect and measure the water depth. And obtaining the average flow velocity of the cross section according to a pre-established mathematical model, and calculating the flow value according to the actual flow area of the river channel.|[0101] S3, acquiring real-time water quality information|[0102] Carbon dioxide gas-sensitive electrodes of a multi-channel ion potentiometer are arranged at the left, middle and right three points of the monitored section, and the water temperature and HCO of each point on the section are monitored in real time through the Nernst equation and the carbonic acid balance principle 3- And (4) concentration. The left and right points are respectively arranged at 1m-2m off-shore with obvious water flow, and the middle point can be arranged on a Chinese body line.|[0103] In addition, during this period, the operator analyzed Ca on the monitored section by ion electrode or laboratory in a manner of 1 time/month 2+ 、Mg 2+ 、HCO 3- And (3) measuring, wherein the monitoring points are the same as the hydrological water quality monitoring points, and the result is as follows: in water (Ca) 2+ +Mg 2+ ) With HCO 3- The equivalent ratio of (a) to (b) is between 1 and 1.05, the evaluation can be continued using this example.|[0104] S4, calculating CO 2 Consuming flux|[0105] The data obtained in the steps S2 and S3 are integrated according to the monthly time period to obtain the monthly mean flow and HCO 3- And (4) concentration, and further obtaining the monthly karst weathering CO2 consumption flux of the Puzi river basin, which is shown in the table below. Karst weathering CO of Puzi river basin 2 The consumed flux was 80717.95t/a.|[0106] |[0107] |[0108] S5, calculating the carbon sink strength|[0109] And substituting the karst CO2 consumption flux 80717.95 (t/a) and the area 801km2 of the basin into a basin carbon sink strength calculation formula to calculate the basin carbon sink strength 100.8 (t/km2. A).|[0110] The third embodiment:|[0111] as shown in fig. 2, a carbon sequestration capacity assessment device based on watershed scale karst weathering is characterized in that: the method comprises the following steps:|[0112] the drainage basin dividing module 11 is used for extracting a river network and dividing water catchment units based on digital elevation model data by adopting a GIS technology to finish drainage basin division;|[0113] the monitoring section setting module 12 is used for integrating the distribution conditions of the existing automatic water quality monitoring stations and hydrological stations and automatically screening monitoring sections;|[0114] the data acquisition module 13 comprises acquisition hydrological information 131 and acquisition water quality information 132, wherein the hydrological information includes but is not limited to section area, section flow, water flow rate, water surface elevation and water flow direction, and the water quality information includes but is not limited to pH value and water temperature;|[0115] the data processing module 14 is used for matching effective hydrological information and water quality information data, deleting redundant and abnormal data and calculating HCO 3- Concentration, CO2 consumption flux;|[0116] and the evaluation module 15 generates a karst carbon sink strength report of the watershed scale.|[0117] In this embodiment, when selecting specific basin, then can divide according to the basin and select corresponding monitoring section automatically to can read the data that hydrology monitor and the water quality monitoring appearance that correspond on the monitoring section gathered through data acquisition module. The data processing module can process data according to an input instruction of an operator, and the matched effective data is ready for calculation. In the evaluation module, CO is generated according to information such as hydrology, water quality and the like 2 Consumption flux, watershed carbon sink strength evaluation report.|[0118] Preferably, in the drainage basin dividing module 11, a drainage basin with small human activity influence should be selected as a monitoring object, that is, SO 2 、NO 2 And the like, less contaminated watersheds. Ion electrode and laboratory analysis can be selected in advance for Ca in water 2+ 、Mg 2+ 、HCO 3- Plasma measurement of (Ca) in water 2+ +Mg 2+ ) With HCO 3- Should be 1. + -. 0.05. Otherwise the present evaluation device is not applicable.|[0119] Preferably, in the monitoring section setting module 12, a drainage basin outlet section which is overlapped with an existing hydrological station or an existing automatic water quality monitoring station can be selected as a monitoring section; if no corresponding station exists, the position with straight river channel, smooth water flow and regular river bed within the range of 2km at the drainage basin outlet can be selected.|[0120] Preferably, in the data acquisition module 13, ca in the water body should be acquired 2+ 、Mg 2+ 、HCO 3- To calculate (Ca) in the water body 2+ +Mg 2+ ) With HCO 3- The equivalent ratio of (a).|[0121] Preferably, in the data processing module 14, the (Ca) in the water body is detected 2+ +Mg 2+ ) With HCO 3- Whether the equivalent ratio of (A) is within 1 + -0.05, and generating a corresponding prompt report to verify HCO 3- The effectiveness of (c).|[0122] The fourth embodiment:|[0123] as shown in fig. 4, a computer-readable storage medium 31 stores a computer program, which when executed by one or more processors can implement the carbon sequestration capacity assessment method based on basin scale karstic weathering as described in any one of the first embodiments.|[0124] In this embodiment, the computer program may be divided into one or more modules, and these modules may be a series of computer program instruction segments capable of performing specific functions as described in the first embodiment and the third embodiment, and the instruction segments are used for describing the processes executed by the computer program. The storage medium may be a magnetic disk storage and an optical storage.|[0125] The foregoing is a more detailed description of the present invention in connection with specific preferred embodiments thereof, and it is not intended that the specific embodiments of the present invention be limited to these descriptions. Other embodiments that can be derived by a person skilled in the art without departing from the scope of the present invention are also intended to be included within the scope of the present invention. Family Number|(103959807)|103959807|Abstract|(CN115728223 A)|The invention is suitable for the technical field of carbon sink monitoring , and provides a carbon sink capacity assessment method , device and system based on watershed scale karst weathering and a medium . Acquiring real - time hydrological information ; acquiring real - time water quality information ; calculating the CO2 consumption flux ; calculating the carbon sink strength ; the device comprises a drainage basin division module ; a monitoring section setting module ; a data acquisition module ; a data processing module ; and an evaluation module . The invention creatively provides the carbon sink capacity assessment method , device and system based on the drainage basin scale karst weathering and the medium , and provides a new research direction for dynamic monitoring and quantitative calculation in the karst carbon sink weathering process . The hydrological information data and the water quality information data can be continuously collected and processed in real time , synchronous and high - resolution data are obtained , and the timeliness and accuracy of carbon sink capacity evaluation can be effectively guaranteed . |IPC codes|(CN115728223 A)|G01C - 013/00 |G01D - 021/02 |G01N - 017/00 |G01N - 033/18 |Title|(CN115728223 A)|Carbon sequestration capability assessment method , device and system based on watershed scale karst weathering , and medium | Analysis of biological materials Y02A-020/152 Y02A-020/152 G01C-013/00|G01D-021/02|G01N-017/00|G01N-033/18 G01C-013/00|G01D-021/02|G01N-017/00|G01N-033/18 CN115235560|CN103175943|CN113687042|CN106548408 CN115235560 102264928 WHO=Examiner SELF=N CAT=Y|CN103175943 45522349 WHO=Examiner SELF=N CAT=Y|CN113687042 97157123 WHO=Examiner SELF=N CAT=A|CN106548408 75770804 WHO=Examiner SELF=N CAT=A 黄真理: &quot;《中国环境水力学 2002》&quot;, vol. 1, 31 October 2002, 中国水利水电出版社, pages: 280 - 287 (Cat. Y)|查小森 等: &quot;短时间尺度下岩溶泉碳汇效应研究――以重庆金佛山水房泉为&quot;, 《地下水》, vol. 37, no. 2, 31 March 2015 (2015-03-31), pages 42 - 45 (Cat. Y) CN103175943; CN106548408; CN113687042; CN115235560 PENDING (CN115728223)|PENDING ALIVE (CN115728223)|ALIVE (CN115728223)|LEGAL DETAILS FOR CN115728223|Actual or expected expiration date=2042-12-07|Legal state=ALIVE|Status=PENDING|Event publication date=2022-12-07|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211564985|Application date=2022-12-07|Standardized application number=2022CN-1564985|Event publication date=2023-03-03|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115728223|Publication stage code=A|Publication date=2023-03-03|Standardized publication number=CN115728223|Event publication date=2023-03-03|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-03-21|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN115728223)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQOonDaLqka0Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000066799018&ekey=2195&xpn=CN115728223&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=QgoIVzQ5uMWCD9eGr%252BNPi5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN115728223)|CN (CN115728223)|NAME=CHONGQING ECOLOGICAL ENV MONITORING CENTER , COUNTRY=CN (CN115728223)|NAME=XU WEIWEI;CHONGQING XINHANG INTELLECTUAL PROPERTY AGENCY CO. LTD. , REG=50218 (CN115728223)|NAME=QIN CHENG|NAME=DENG LI|NAME=LIU HAO|NAME=LIU NIAN|NAME=CAI YU|NAME=GE MIAO|NAME=YANG BING|NAME=HU QIYAO|NAME=GONG LI|NAME=JIANG JING|NAME=TANG XIAO|NAME=YU HANG 0 1 Titre: (CN115728223)|Carbon sequestration capability assessment method, device and system based on watershed scale karst weathering, and medium Résumé: (CN115728223)|The invention is suitable for the technical field of carbon sink monitoring, and provides a carbon sink capacity assessment method, device and system based on watershed scale karst weathering and a medium. Acquiring real-time hydrological information; acquiring real-time water quality information; calculating the CO2 consumption flux; calculating the carbon sink strength; the device comprises a drainage basin division module; a monitoring section setting module; a data acquisition module; a data processing module; and an evaluation module. The invention creatively provides the carbon sink capacity assessment method, device and system based on the drainage basin scale karst weathering and the medium, and provides a new research direction for dynamic monitoring and quantitative calculation in the karst carbon sink weathering process. The hydrological information data and the water quality information data can be continuously collected and processed in real time, synchronous and high-resolution data are obtained, and the timeliness and accuracy of carbon sink capacity evaluation can be effectively guaranteed. 32 Abstract gpt-4o-mini no The article focuses on assessing carbon sink capacity through monitoring and evaluation methods rather than directly addressing accelerated weathering processes or CO2 capture through mineral alteration.
35 CN202211110693 CN202211110693 CN115517043 103202165 CN115517043 A 2022-12-27 [CN115517043] 2022-09-13 2022-09-13 2022-12-27 (CN115517043)|2042-09-13 (CN115517043)|Phosphogypsum and coal gangue cooperated soil formation and carbon sequestration method (CN115517043)|The invention discloses a method for soil formation and carbon sequestration by synergy of ardealite and coal gangue. The method comprises the following steps: (1) crushing coal gangue; (2) flattening the coal gangue; (3) arranging a drainage ditch; (4) adding ardealite and a modifier, and ploughing; (5) applying a microbial agent: combining spraying and hole application; (6) planting or cultivating plants; (7) maintenance and irrigation: keeping soil humidity, and spraying pesticides on the planted trees in time to prevent plant diseases and insect pests from threatening the growth of the trees; grass felts are laid on herbaceous plants, so that the influence of direct sunlight and high temperature is reduced. The construction method is simple, reasonable in manufacturing cost, rapid in greening aging, wide in application range and easy to construct, coal gangue and ardealite can be effectively utilized, waste utilization is achieved, the survival rate of trees can reach 92% or above, the survival rate of herbaceous plants can reach 96% or above, the method can be applied to soil engineering of different coal mine areas, and the application range is wide. And the method has high generalization performance and applicability. KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY (CN115517043)|KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) HUANG JIANHONG|SHU JUNYU|ZHAO YUNGE|ZUO JIANFEN|TIAN SENLIN|HU XUEWEI|ZHAO QUN|CUI XIANGFEN (CN115517043)|HUANG JIANHONG|SHU JUNYU|ZHAO YUNGE|ZUO JIANFEN|TIAN SENLIN|HU XUEWEI|ZHAO QUN|CUI XIANGFEN (CN115517043)|ZHANG YU;Kunming Tongju Patent Agency Co., Ltd.|Reg. Nb: 53214 (CN115517043)|The stacking of the coal gangue not only causes a great deal of land waste, but also causes a serious environmental pollution problem.| (CN115517043)|1. The method for realizing the soil formation and carbon sequestration of the phosphogypsum and the coal gangue is characterized by comprising the following steps of:(1) Crushing the coal gangue with the particle size of more than 25 mm;(2) Leveling the crushed coal gangue, and digging drainage channels at two sides of a road of a leveled land block;(4) Applying phosphogypsum and a modifier on the surface of the coal gangue, and ploughing to fully mix the phosphogypsum, the modifier and the coal gangue together;(5) Applying a microbial agent: hole application of a microbial agent is used for woody plants; herbal drenching and applying a microbial agent;(6) Planting or planting a plant;(7) Irrigation and maintenance: irrigating in time to keep soil humidity, and sealing holes after watering trees; laying a turf felt for the herbaceous plant in the sprouting and seedling stage, moisturizing and relieving the influence of high temperature.| (CN115517043)|The invention aims to provide a method for realizing soil formation and carbon sequestration of coal gangue by cooperation of ardealite and ardealite. The purpose of the invention is realized by the following technical scheme: a method for realizing soil formation and carbon sequestration by using phosphogypsum and coal gangue comprises the following steps:|The invention discloses a method for realizing soil formation and carbon sequestration by using phosphogypsum and coal gangue, which comprises the following steps: (1) crushing coal gangue; (2) leveling the coal gangue; (3) arranging a drainage ditch; (4) adding phosphogypsum and modifying agent and ploughing; (5) applying a microbial agent: combining drenching application and hole application; (6) planting or cultivating plants; (7) maintaining and irrigating: the soil humidity is kept, and pesticides are sprayed on the planted trees in time to prevent diseases and insect pests from threatening the growth of the trees; and a grass felt is laid on the herbaceous plants, so that the direct sunlight and high-temperature influence is reduced.| (CN115517043)|COAL GANGUE(100,40)|CARBON SEQUESTRATION(100,14)|SOIL FORMATION(100,2)|GANGUE SOIL FORMATION(100,1)|PHOSPHOGYPSUM CARBON SEQUESTRATION(100,1)|COAL GANGUE CARBON SEQUESTRATION(52,3)|COAL GANGUE STACKING(52,1)|CRUSHED COAL GANGUE(46,2)|PHOSPHOGYPSUM(45,32)|CRUSHING COAL GANGUE(43,3)|PHOSPHOGYPSUM COAL GANGUE(39,2)|TREE PLANTING(39,1)|SOIL HUMIDITY(38,3)|PHOSPHOGYPSUM COOPERATION(38,2)|ARDEALITE COOPERATION(34,1)|GRASS FELT(34,1)|TURF FELT(34,1)|WOODY PLANT(33,5)|DRY STRAW MAT(30,2)|PHOSPHOGYPSUM SYNERGISM(30,1)|WATERING TREE(28,2)|LAND DEAL(28,1)|HERBACEOUS PLANT(27,18)|REALIZING SOIL FORMATION(26,5)|GROUND LEVEL BLOCK(26,1)|DRENCHING(25,1)|COAL GANGUE SOIL CHEMICAL(24,1)|DUG HOLE(23,8)|DRAINAGE DITCH(22,20)|SUNLIGHT(22,1)|ADDING PHOSPHOGYPSUM(21,3)|CULTIVATING SHRUB(21,2)|APPLYING PHOSPHOGYPSUM(20,2)|PHOSPHOGYPSUM PAVING THICKNESS(19,3)|PESTICIDE(19,1)|INSECT PEST(18,1)|MODIFIER(17,19)|GROUND BALL(16,13)|PLANTING(16,9)|SEEDLING RAISING(16,2)|SHRUB PLANT(16,2)|SPROUT(16,2)|HERBAL(16,1)|POURING CONCRETE(15,5)|PLOWING(15,2)|ARDEALITE(15,1)|SEEDLING(14,10)|NURSERY STOCK(14,5)|BACILLUS MUCILAGINOSUS SEEDLING(14,3)|LAND UTILIZATION(14,2)|DISEASE PREVENTION(14,1)|PLOWED COAL GANGUE(13,3)|ENVIRONMENTAL POLLUTION(13,1)|SOIL CHEMICAL CONVERSION(13,1)|FESTUCA ARUNDINACEA(12,15)|COAL GANGUE SURFACE(12,3)|IRRIGATION(12,3)|POPULARIZATION(11,3)|PLASTIC PARTITION(10,5)|FIXING CARBON(10,1)|DRAINAGE CHANNEL(9,2)|GERMINATION(9,2)|HERBACEOUS PLANT SURVIVAL RATE(9,2)|SOIL IMPROVEMENT(9,2)|TREE SURVIVAL RATE(9,2)|COAL GANGUE SOIL FERTILITY(9,1)|SEA BUCKTHORN(8,8)|DOWNWARD DEPTH(8,5)|FOUNDATION(8,5)|PLUM BLOSSOM SHAPE(8,5)|SAPLING(8,5)|GRASS SEED SOWING(8,4)|CRUSHED PHOSPHOGYPSUM(8,3)|PAVED PHOSPHOGYPSUM THICKNESS(8,3)|TAMPING SOIL BALL(8,3)|SOIL ENGINEERING(8,2)|COAL GANGUE COMPREHENSIVE UTILIZATION(8,1)|PHOSPHOGYPSUM LAYER(7,9)|CHICKEN MANURE DECOMPOSITION(7,3)|PURCHASING NURSERY(7,3)|SEEDLING SHORTAGE(7,3)|MANUFACTURING COST(7,2)|SPHAEROTHECA PERSICA(7,2)|COAL GANGUE RESOURCE UTILIZATION(7,1)|COAL GANGUE SOIL UTILIZATION(7,1)|ORGANIC FERTILIZER(6,11)|AMORPHA FRUTICOSA SURVIVAL RATE(6,6)|DRY GRASS MAT(6,6)|KOCHIA SCOPARIA SURVIVAL RATE(6,6)|GRASS MAT HUMIDITY(6,3)|SEA BACKTHERN(6,3)|CLIMATE TEMPERATURE CONDITION(6,2)|COAL MINE AREA(6,2)|CROSS EXCAVATION(6,2)|PHOSPHOGYPSUM PARTICLE SIZE(6,2)|SOWN(6,2)|WATER OUTLET PLANE(6,2)|ACCUMULATED COAL GANGUE(6,1)|COAL GANGUE HILL(6,1)|SILICATE MICROBIAL INOCULUM(6,1)|COAL GANGUE LAYER SURFACE(5,5)|PARTITION PLATE TOTAL HEIGHT(5,5)|PARTICLE SIZE(5,4)|PLANTING PLANT(5,3)|SEED BUD(5,2)|CALLIOPSIS JAVANICA(5,1)|COSMOS CHINENSIS(5,1)|GEOLOGICAL DISASTER(5,1)|NONPROFESSIONAL PLANTING(5,1)|GROUND COVER(4,3)|PIT DEPTH(4,3)|WET GRASS MAT(4,3)|FORMED WASTE UTILIZATION(4,2)|COAL RESOURCE SUSTAINABLE DEVELOPMENT(4,1)|KOCHIA SCOPARIA CULTIVATION PERIOD(4,1)|SILICATE BACTERIUM(4,1)|SPROUTING SEED(4,1)|TIMELY REPLANTING(4,1)|SQUARE METER(3,6)|BIOCHAR(3,4)|LANDFORM(3,3)|MODIFIER LAYER(3,3)|APPLICATION DEPTH(3,2)|SIGNIFICANCE(3,2)|WATER TIME INTERVAL(3,2)|ECOLOGICAL ENVIRONMENT(3,1)|EXTENSIVE UTILIZATION(3,1)|GREEN MINING(3,1)|HARMFUL SOLUBLE SALT(3,1)|HERBACEOUS PLANT GROWTH(3,1)|HIGH TEMPERATURE INFLUENCE(3,1)|MAINTENANCE PERSONNEL(3,1)|MOISTURE PRESERVATION(3,1)|MOUNTAIN COLLAPSE(3,1)|NATIONAL ENTERPRISE(3,1)|PERFECT DRAINAGE(3,1)|RESOURCE RECYCLING(3,1)|STACK ACCUMULATION(3,1)|UNDERGROUND SOIL(3,1)|HERBACEOUS PLANT SEED(2,2)| (CN115517043)|1. The method for realizing the soil formation and carbon sequestration of the phosphogypsum and the coal gangue is characterized by comprising the following steps of:|(1) Crushing the coal gangue with the particle size of more than 25 mm;|(2) Leveling the crushed coal gangue, and digging drainage channels at two sides of a road of a leveled land block;|(4) Applying phosphogypsum and a modifier on the surface of the coal gangue, and ploughing to fully mix the phosphogypsum, the modifier and the coal gangue together;|(5) Applying a microbial agent: hole application of a microbial agent is used for woody plants; herbal drenching and applying a microbial agent;|(6) Planting or planting a plant;|(7) Irrigation and maintenance: irrigating in time to keep soil humidity, and sealing holes after watering trees; laying a turf felt for the herbaceous plant in the sprouting and seedling stage, moisturizing and relieving the influence of high temperature.|2. The method for the phosphogypsum-coal gangue soil chemical conversion and carbon sequestration cooperated with the phosphogypsum according to claim 1, is characterized in that the depth of the drainage ditch is 40cm, the width of the drainage ditch is 50cm, and a foundation is tamped; pouring concrete on two sides of the road and two sides and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm higher than the water outlet plane.|3. The method for realizing the soil improvement and the carbon sequestration of the coal gangue by using the phosphogypsum in cooperation with the phosphogypsum according to claim 1, wherein the phosphogypsum and the modifying agent are paved on the surface of the coal gangue layer, and the paving thickness of the phosphogypsum is 10cm; the modifier is a mixture of biological carbon, organic fertilizer and biological straw, and the volume ratio is 6:2:2 to 4:2:2, paving the phosphogypsum and then the modifying agent, and turning over till the depth is more than 60cm after paving, so that the coal gangue, the phosphogypsum and the modifying agent are fully mixed.|4. The method for the cooperation of the phosphogypsum and the coal gangue for the soil chemical and carbon sequestration of the claim 1, wherein the particle size of the phosphogypsum is less than or equal to 5mm.|5. The method for the synergism of phosphogypsum and coal gangue soil chemical and carbon sequestration as claimed in claim 1, wherein the microbial agent is bacillus mucilaginosus.|6. The method for realizing the soil improvement and the carbon sequestration of the coal gangue by using the phosphogypsum in cooperation with the coal gangue as per claim 1, wherein the microbial agents and the herbaceous plants are applied by spraying after being sown, the application amount is 0.5kg/100 square meter, and a turf is covered immediately after the application; for woody plants 50 g/hole, at a distance of 5cm from the sapling, the application depth was 20cm.|7. The method for improving soil and fixing carbon by using phosphogypsum and coal gangue in cooperation with the phosphogypsum as claimed in claim 1, wherein the usage amount of the seeds of the herbaceous plants is planted according to the density of 15g per square meter; and (3) cultivating shrubs, namely 1 hole per square meter per nursery stock, wherein the diameter of each dug hole is 0.9m, the depth of each dug hole is 0.6m, the cross excavation is in a plum blossom shape, for the nursery stocks with soil, the diameter of each dug hole is 35-50cm greater than the diameter of a soil ball, and the depth of each dug hole is 5-10cm deeper than the height of the soil ball.|8. The method for the phosphogypsum-coal gangue soil-ification and carbon sequestration cooperated with the phosphogypsum as claimed in claim 1, is characterized in that a dry straw mat needs to be laid on the surface of a herbaceous plant during seedling raising, the dry straw mat is removed after germination, a straw mat with the thickness of 2cm and the humidity of 70% is laid, and the straw mat is removed when seedlings grow to 6-8 cm; when the woody plant is irrigated, the specific watering time interval and the watering quantity are customized according to the specific climate temperature condition and the conditions of illumination and water evaporation quantity.|9. The method for improving the soil utilization and fixing the carbon of the coal gangue through the cooperation of the phosphogypsum and the coal gangue as claimed in claim 1, wherein the shrub plant is any one or more of amorpha fruticosa and sea buckthorn, and the herbaceous plant is any one or more of kochia scoparia, cosmos and festuca arundinacea. (CN115517043)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of environmental protection, and particularly relates to a method for realizing soil formation and carbon sequestration by using phosphogypsum and coal gangue.|BACKGROUND ART|[0002] During the coal mining, processing and using processes, a large amount of solid waste coal gangue is produced. The coal gangue is one of the largest industrial solid wastes in the discharge amount and the accumulated stacking amount of China at present. The stacking of the coal gangue not only causes a great deal of land waste, but also causes a serious environmental pollution problem. Harmful soluble salt and toxic heavy metal generated by weathering of the coal gangue can cause underground soil and water along with leaching and infiltration of rainwater, so that soil salinization is caused, growth of crops is influenced, water pollution endangers the health of human bodies and other organisms, and a large amount of toxic and harmful gas generated by spontaneous combustion of the accumulated coal gangue seriously pollutes the atmosphere and seriously threatens the health of residents near the deposit bottom. In addition, due to natural accumulation, the coal gangue hills are loose in structure and poor in stability, so that geological disasters such as mountain collapse, landslide and debris flow are caused frequently, and national enterprises need to invest a large amount of funds to solve the problems, so that resource utilization of the coal gangue is an effective way for treating the coal gangue, and the method has extremely important significance for realizing green mining, resource recycling and sustainable development of coal resources.|[0003] Based on the above, a method for combining phosphogypsum with coal gangue to realize soil formation and carbon sequestration needs to be invented.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a method for realizing soil formation and carbon sequestration of coal gangue by cooperation of ardealite and ardealite.|[0005] The purpose of the invention is realized by the following technical scheme: a method for realizing soil formation and carbon sequestration by using phosphogypsum and coal gangue comprises the following steps:|(1) Crushing coal gangue: crushing coal gangue with large particle size (particle size >25 mm)|(2) Leveling the coal gangue: flattening the crushed coal gangue in a factory|(3) Arranging a ditch for draining: digging drainage channels at two sides of road|(4) Applying phosphogypsum and a modifier and ploughing: and applying the phosphogypsum and the modifying agent on the surface of the coal gangue, and ploughing to fully mix the phosphogypsum, the modifying agent and the coal gangue together.|[0006] (5) Applying a microbial agent: the hole application microbial inoculum is combined with a small amount of broadcast application microbial inoculum|(6) Planting or planting plants|(7) Irrigation and maintenance: irrigating in time to keep soil humidity, and sealing holes after watering trees; laying a straw mat for the sprouting and seedling stage of the herbaceous plant, preserving moisture and reducing the influence of high temperature.|[0007] Further, the paving thickness of the phosphogypsum and the phosphogypsum is 10cm; the modifier is biological carbon, organic fertilizer and biological straw, and is prepared from the following raw materials in a volume ratio of 6:2:2 to 4:2:2, mixing the components, and paving the components to a thickness of 4cm; the microbial agent is bacillus mucilaginosus.|[0008] Furthermore, the phosphogypsum and the modifying agent are paved on the surface of the coal gangue layer, and the paving thickness of the phosphogypsum is 10cm; the modifier is a mixture of biological carbon, organic fertilizer and biological straw, and the volume ratio is 5:2:2, paving the phosphogypsum and then the modifying agent, and ploughing the mixture after paving the phosphogypsum and the modifying agent to a depth of over 60cm so as to fully mix the coal gangue, the phosphogypsum and the modifying agent.|[0009] Furthermore, the phosphogypsum is crushed phosphogypsum particles, and the particle size of the phosphogypsum is less than or equal to 5mm.|[0010] Furthermore, the drainage ditch means that the depth of the ditch is 40cm, the width of the ditch is 50cm, and a foundation is tamped; pouring concrete on two sides of the road, two sides of the drainage ditch and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm above the water level.|[0011] Further, the microbial agent is bacillus mucilaginosus.|[0012] Further, the microbial agent is applied to the square meter in a spraying manner after being sown, the application rate is 0.2 to 0.8kg/100 square meter, and a straw mat is covered immediately after application; for woody plants 50 g/hole, at a distance of 5cm from the sapling, the application depth was 20cm.|[0013] Further, the usage amount of the herbaceous plant seeds is planted according to the density of 15g per square meter; and (3) cultivating shrubs, namely 1 hole per square meter per nursery stock, wherein the diameter of each dug hole is 0.9m, the depth of each dug hole is 0.6m, the cross excavation is in a plum blossom shape, for the nursery stocks with soil, the diameter of each dug hole is 35-50cm greater than the diameter of a soil ball, and the depth of each dug hole is 5-10cm deeper than the height of the soil ball.|[0014] Furthermore, a dry grass mat needs to be laid on the surface of the herbaceous plant during seedling raising, the dry grass mat is removed after germination, a grass mat with the thickness of 2cm and the humidity of 70% is laid, and the grass mat is removed when the seedling grows to 7 cm; when the woody plant is irrigated, the specific watering time interval and the watering amount are customized according to the specific climate temperature condition and the conditions of illumination and water evaporation amount.|[0015] Further, the shrub plants are amorpha fruticosa and hippophae rhamnoides, and the herbaceous plants are kochia scoparia, cosmos chinensis and festuca arundinacea.|[0016] Further, the organic fertilizer is chicken manure which is fermented and decomposed in the market; the biochar is a powdery biological organic material sold in the market; the straws are common straws, and the length of the straws is 2cm; the silicate microbial inoculum is bacillus mucilaginosus sold in the market.|[0017] The invention has the beneficial effects that:|(1) Opens up a new way for recycling the coal gangue and the phosphogypsum and has important significance for improving the comprehensive utilization of the coal gangue and the phosphogypsum.|[0018] (2) The method has strong applicability, can be applied to greening planting of the soil utilization of the coal gangue in different areas, and has strong applicability and popularization.|[0019] (3) The method has simple steps, is easy to operate and execute, has easily obtained required raw materials, low price and low comprehensive cost, and is also suitable for non-professional planting and maintenance personnel.|[0020] (4) A perfect drainage and irrigation system is established by constructing a drainage channel, so that the drainage and irrigation is ensured to be smooth and unobstructed, the requirement of irrigation can be met in dry seasons, drainage can be timely carried out in rainy seasons, the water accumulation in coal gangue soil experimental fields is prevented, and the drainage is ensured to be smooth and unobstructed especially in heavy rain days.|[0021] (5) According to the method, a large number of shrubs and herbaceous plants are screened, and the results show that amorpha fruticosa, sea buckthorn, kochia scoparia, calliopsis javanica and Festuca arundinacea are obtained, and the plant varieties have high tolerance to coal gangue, can adapt to local ecological environment, and effectively improve the survival rate of the plants.|[0022] (6) The modifier used in the method contains organic fertilizer, so that the fertility of the coal gangue soil is improved, and the silicate bacteria are guaranteed to have enough nutrients to grow and reproduce.|[0023] (7) The modifier can well increase the content of organic matters in the coal gangue and meet the basic requirements of animal and plant growth in soil.|[0024] (8) In the method, the residue of the plant is left in the plant after a life cycle, so that the carbon content in the coal gangue soil is increased, and carbon in the atmosphere can be effectively fixed in the soil.|INVENTION MODE|Detailed Description|[0025] The present invention is further illustrated but not limited in any way by the following description, and any alterations or substitutions based on the teachings of the present invention are intended to fall within the scope of the present invention.|[0026] Example 1: method for realizing soil formation and carbon sequestration by using phosphogypsum and coal gangue|Crushing large-particle coal gangue;|step two, paving the crushed phosphogypsum in a field;|leveling the field to level the surface of the field;|step four, arranging a drainage ditch: the depth of the ditch is 40cm, the width is 50cm, and the foundation is tamped; pouring concrete on two sides of the road, two sides of the drainage ditch and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm above the water level.|[0027] Step five, adding phosphogypsum and a modifier: paving a phosphogypsum layer and a modifier on the surface of the coal gangue layer, wherein the thickness of the paved phosphogypsum is 10cm, the modifier is biological carbon, organic fertilizer and biological straw, and the volume ratio of the modifier to the phosphogypsum layer is 4:2:2, and the paving thickness is 4cm. And after the phosphogypsum layer and the modifier layer are laid, ploughing to uniformly distribute the phosphogypsum and the modifier in the coal gangue layer. Then planting plants, adopting a cultivation method for shrubs, manually digging pits on the ploughed coal gangue according to the density of 1 pit per square meter per sapling, wherein the diameter of each pit is 0.9m, the pit depth is 0.6m, the pits are in a plum blossom shape through cross excavation, purchasing nursery stocks with soil balls, the diameter of each soil ball is not more than 40cm, the height of each soil ball is less than 50cm, the shrubs are amorpha fruticosa and sea buckthorn, and checking whether the nursery stocks are qualified before planting, if the branches are complete, whether the nursery stocks reach the standard. Tamping soil balls after cultivation, finishing the landform, applying 50 g/seedling of Bacillus mucilaginosus in a hole with the depth of 20cm at a position 5cm away from the seedlings, and immediately covering soil after application. Selecting Kochia scoparia, callistephus and Festuca arundinacea for herbaceous plants, sowing the grass seeds at a rate of 15g per square meter, performing spray application of Bacillus mucilaginosus at a rate of 0.5kg per 100 square meters after sowing the grass seeds, and immediately covering dry grass mats after application.|[0028] The organic fertilizer is fermented and decomposed chicken manure sold in the market; the biochar is a powdery biological organic material sold in the market; the straws are common straws and the length of the straws is 2cm.|[0029] Step six, maintenance: in summer, the temperature is high, the evaporation of water on the surface layer of the soil is fast, the growth and development of herbaceous plants are not facilitated, in order to reduce the water loss and the temperature of the surface layer of the soil, dry grass mats are paved on the surface of the soil during the cultivation period of the Kochia scoparia, the Calliopsis and the Festuca arundinacea, wet grass mats with the thickness of 2cm are replaced after the seeds bud, the humidity of the grass mats is kept at 70%, and the grass mats are removed when the seedlings grow to 7 cm. And timely reseeding the planting points with seedling shortage.|[0030] The survival rate of amorpha fruticosa and sea buckthorn can reach 92%, and the survival rate of Kochia scoparia, calliopsis and Festuca arundinacea can reach 96%.|[0031] Example 2:|crushing large-particle coal gangue;|step two, paving the crushed phosphogypsum in a field;|leveling the field to level the surface of the field;|step four, arranging a drainage ditch: the depth of the ditch is 40cm, the width is 50cm, and the foundation is tamped; pouring concrete on two sides of the road, two sides of the drainage ditch and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm higher than the water outlet plane.|[0032] Step five, adding the phosphogypsum and the modifying agent: paving a phosphogypsum layer and a modifier on the surface of the coal gangue layer, wherein the thickness of the paved phosphogypsum is 10cm, the modifier is biological carbon, organic fertilizer and biological straw, and the volume ratio of the modifier to the phosphogypsum layer is 5:2:2, and the paving thickness is 4cm. And after the phosphogypsum layer and the modifier layer are laid, ploughing to uniformly distribute the phosphogypsum and the modifier in the coal gangue layer. Then planting plants, adopting a cultivation method for shrubs, manually digging pits on the ploughed coal gangue according to the density of 1 pit per square meter per sapling, wherein the diameter of each pit is 0.9m, the pit depth is 0.6m, the pits are in a plum blossom shape through cross excavation, purchasing nursery stocks with soil balls, the diameter of each soil ball is not more than 40cm, the height of each soil ball is less than 50cm, the shrubs are amorpha fruticosa and sea buckthorn, and checking whether the nursery stocks are qualified before planting, if the branches are complete, whether the nursery stocks reach the standard. Tamping soil balls after cultivation, finishing the landform, applying 50 g/seedling of Bacillus mucilaginosus in a hole with the depth of 20cm at the position 5cm away from the seedlings, and immediately covering soil after application. The method is characterized in that the Kochia scoparia, the cosmos and the festuca arundinacea are selected for herbaceous plants, the grass seed sowing amount is 15g per square meter, the bacillus mucilaginosus is applied by spraying after the grass seed sowing, the application amount is 0.5kg per 100 square meters, and the grass mat is immediately covered after the application.|[0033] The organic fertilizer is fermented and decomposed chicken manure sold in the market; the biochar is a powdery biological organic material sold in the market; the straws are common straws and the length of the straws is 2cm.|[0034] Step six, maintenance: the temperature is high in summer, the water in the surface layer of the soil is quickly evaporated, the herbaceous plant growth and development are not facilitated, in order to reduce the water loss and the temperature of the surface layer of the soil, during the cultivation period of Kochia scoparia, sphaerotheca persica and Festuca arundinacea, dry grass mats are laid on the surface of the soil, wet grass mats with the thickness of 2cm are replaced after the seeds sprout, the humidity of the grass mats is kept at 70%, and the grass mats are removed when the seedlings grow to 7 cm. And timely reseeding the planting points with seedling shortage.|[0035] The survival rate of amorpha fruticosa and sea buckthorn can reach 93%, and the survival rate of Kochia scoparia, calliopsis and Festuca arundinacea can reach 95%.|[0036] Example 3:|crushing large-particle coal gangue;|step two, paving the crushed phosphogypsum in a field;|leveling the field to level the surface of the field;|step four, arranging a drainage ditch: the depth of the ditch is 40cm, the width is 50cm, and the foundation is tamped; pouring concrete on two sides of the road and two sides and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm above the water level.|[0037] Step five, adding phosphogypsum and a modifier: paving a phosphogypsum layer and a modifier on the surface of the coal gangue layer, wherein the thickness of the paved phosphogypsum is 10cm, and the modifier is biological carbon, organic fertilizer and biological straw according to the volume ratio of 6:2:2, and the paving thickness is 4cm. And after the phosphogypsum layer and the modifier layer are laid, ploughing to uniformly distribute the phosphogypsum and the modifier in the coal gangue layer. Then planting plants, adopting a cultivation method for shrubs, manually digging pits on the ploughed coal gangue according to the density of 1 pit per square meter per sapling, wherein the diameter of each pit is 0.9m, the pit depth is 0.6m, the pits are in a plum blossom shape through cross excavation, purchasing nursery stocks with soil balls, the diameter of each soil ball is not more than 40cm, the height of each soil ball is less than 50cm, the shrubs are amorpha fruticosa and sea buckthorn, and checking whether the nursery stocks are qualified before planting, if the branches are complete, whether the nursery stocks reach the standard. Tamping soil balls after cultivation, finishing the landform, applying 50 g/seedling of Bacillus mucilaginosus in a hole with the depth of 20cm at a position 5cm away from the seedlings, and immediately covering soil after application. The method is characterized in that the Kochia scoparia, the cosmos and the festuca arundinacea are selected for herbaceous plants, the grass seed sowing amount is 15g per square meter, the bacillus mucilaginosus is applied by spraying after the grass seed sowing, the application amount is 0.5kg per 100 square meters, and the grass mat is immediately covered after the application.|[0038] The organic fertilizer is fermented and decomposed chicken manure sold in the market; the biochar is a powdery biological organic material sold in the market; the straws are common straws and the length of the straws is 2cm.|[0039] Step six, maintenance: in summer, the temperature is high, the evaporation of water on the surface layer of the soil is fast, the growth and development of herbaceous plants are not facilitated, in order to reduce the water loss and the temperature of the surface layer of the soil, dry grass mats are paved on the surface of the soil during the cultivation period of the Kochia scoparia, the Calliopsis and the Festuca arundinacea, wet grass mats with the thickness of 2cm are replaced after the seeds bud, the humidity of the grass mats is kept at 70%, and the grass mats are removed when the seedlings grow to 7 cm. And timely replanting the planting points with seedling shortage.|[0040] The survival rate of amorpha fruticosa and sea backthern can reach 91%, and the survival rate of kochia scoparia, cosmos and festuca arundinacea can reach 95%.|[0041] Comparative example 1:|the implementation process steps are the same as those of the embodiment 2, but a phosphogypsum layer is not paved on the surface of the coal gangue, and only the modifying agent is paved. The survival rate of amorpha fruticosa and sea backthern is 71%, and the survival rate of kochia scoparia, cosmos and festuca arundinacea is 83%.|[0042] Comparative example 2:|the procedure was carried out in the same manner as in example 2, except that after the cultivation and sowing, bacillus mucilaginosus was not applied. The survival rate of amorpha fruticosa and sea backthern is 56%, and the survival rate of kochia scoparia, cosmos and festuca arundinacea is 68%.|[0043] Comparative example 3:|the procedure was as in example 2, except that no soil was applied to the shrubs after the application of Bacillus mucilaginosus. After the herbaceous plants are sowed, spraying the bacillus mucilaginosus at the application rate of 0.5kg/100 square meter, and covering a dry grass mat every other day after the application. The survival rate of amorpha fruticosa and sea buckthorn is 66%, and the survival rate of Kochia scoparia, sphaerotheca persica and Festuca arundinacea is 78%.|[0044] The construction method provided by the embodiment of the invention is simple, reasonable in manufacturing cost, rapid in greening time effect, wide in application range and simple in construction, can effectively utilize the coal gangue and the phosphogypsum, realizes waste utilization, can achieve the tree survival rate of 91% and the herbaceous plant survival rate of 95%, can be applied to different coal mine area soil engineering, and has strong popularization and application. (CN115517043)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of environmental protection, and particularly relates to a method for realizing soil formation and carbon sequestration by using phosphogypsum and coal gangue.|BACKGROUND ART|[0002] During the coal mining, processing and using processes, a large amount of solid waste coal gangue is produced. The coal gangue is one of the largest industrial solid wastes in the discharge amount and the accumulated stacking amount of China at present. The stacking of the coal gangue not only causes a great deal of land waste, but also causes a serious environmental pollution problem. Harmful soluble salt and toxic heavy metal generated by weathering of the coal gangue can cause underground soil and water along with leaching and infiltration of rainwater, so that soil salinization is caused, growth of crops is influenced, water pollution endangers the health of human bodies and other organisms, and a large amount of toxic and harmful gas generated by spontaneous combustion of the accumulated coal gangue seriously pollutes the atmosphere and seriously threatens the health of residents near the deposit bottom. In addition, due to natural accumulation, the coal gangue hills are loose in structure and poor in stability, so that geological disasters such as mountain collapse, landslide and debris flow are caused frequently, and national enterprises need to invest a large amount of funds to solve the problems, so that resource utilization of the coal gangue is an effective way for treating the coal gangue, and the method has extremely important significance for realizing green mining, resource recycling and sustainable development of coal resources.|[0003] Based on the above, a method for combining phosphogypsum with coal gangue to realize soil formation and carbon sequestration needs to be invented.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a method for realizing soil formation and carbon sequestration of coal gangue by cooperation of ardealite and ardealite.|[0005] The purpose of the invention is realized by the following technical scheme: a method for realizing soil formation and carbon sequestration by using phosphogypsum and coal gangue comprises the following steps:|(1) Crushing coal gangue: crushing coal gangue with large particle size (particle size >25 mm)|(2) Leveling the coal gangue: flattening the crushed coal gangue in a factory|(3) Arranging a ditch for draining: digging drainage channels at two sides of road|(4) Applying phosphogypsum and a modifier and ploughing: and applying the phosphogypsum and the modifying agent on the surface of the coal gangue, and ploughing to fully mix the phosphogypsum, the modifying agent and the coal gangue together.|[0006] (5) Applying a microbial agent: the hole application microbial inoculum is combined with a small amount of broadcast application microbial inoculum|(6) Planting or planting plants|(7) Irrigation and maintenance: irrigating in time to keep soil humidity, and sealing holes after watering trees; laying a straw mat for the sprouting and seedling stage of the herbaceous plant, preserving moisture and reducing the influence of high temperature.|[0007] Further, the paving thickness of the phosphogypsum and the phosphogypsum is 10cm; the modifier is biological carbon, organic fertilizer and biological straw, and is prepared from the following raw materials in a volume ratio of 6:2:2 to 4:2:2, mixing the components, and paving the components to a thickness of 4cm; the microbial agent is bacillus mucilaginosus.|[0008] Furthermore, the phosphogypsum and the modifying agent are paved on the surface of the coal gangue layer, and the paving thickness of the phosphogypsum is 10cm; the modifier is a mixture of biological carbon, organic fertilizer and biological straw, and the volume ratio is 5:2:2, paving the phosphogypsum and then the modifying agent, and ploughing the mixture after paving the phosphogypsum and the modifying agent to a depth of over 60cm so as to fully mix the coal gangue, the phosphogypsum and the modifying agent.|[0009] Furthermore, the phosphogypsum is crushed phosphogypsum particles, and the particle size of the phosphogypsum is less than or equal to 5mm.|[0010] Furthermore, the drainage ditch means that the depth of the ditch is 40cm, the width of the ditch is 50cm, and a foundation is tamped; pouring concrete on two sides of the road, two sides of the drainage ditch and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm above the water level.|[0011] Further, the microbial agent is bacillus mucilaginosus.|[0012] Further, the microbial agent is applied to the square meter in a spraying manner after being sown, the application rate is 0.2 to 0.8kg/100 square meter, and a straw mat is covered immediately after application; for woody plants 50 g/hole, at a distance of 5cm from the sapling, the application depth was 20cm.|[0013] Further, the usage amount of the herbaceous plant seeds is planted according to the density of 15g per square meter; and (3) cultivating shrubs, namely 1 hole per square meter per nursery stock, wherein the diameter of each dug hole is 0.9m, the depth of each dug hole is 0.6m, the cross excavation is in a plum blossom shape, for the nursery stocks with soil, the diameter of each dug hole is 35-50cm greater than the diameter of a soil ball, and the depth of each dug hole is 5-10cm deeper than the height of the soil ball.|[0014] Furthermore, a dry grass mat needs to be laid on the surface of the herbaceous plant during seedling raising, the dry grass mat is removed after germination, a grass mat with the thickness of 2cm and the humidity of 70% is laid, and the grass mat is removed when the seedling grows to 7 cm; when the woody plant is irrigated, the specific watering time interval and the watering amount are customized according to the specific climate temperature condition and the conditions of illumination and water evaporation amount.|[0015] Further, the shrub plants are amorpha fruticosa and hippophae rhamnoides, and the herbaceous plants are kochia scoparia, cosmos chinensis and festuca arundinacea.|[0016] Further, the organic fertilizer is chicken manure which is fermented and decomposed in the market; the biochar is a powdery biological organic material sold in the market; the straws are common straws, and the length of the straws is 2cm; the silicate microbial inoculum is bacillus mucilaginosus sold in the market.|[0017] The invention has the beneficial effects that:|(1) Opens up a new way for recycling the coal gangue and the phosphogypsum and has important significance for improving the comprehensive utilization of the coal gangue and the phosphogypsum.|[0018] (2) The method has strong applicability, can be applied to greening planting of the soil utilization of the coal gangue in different areas, and has strong applicability and popularization.|[0019] (3) The method has simple steps, is easy to operate and execute, has easily obtained required raw materials, low price and low comprehensive cost, and is also suitable for non-professional planting and maintenance personnel.|[0020] (4) A perfect drainage and irrigation system is established by constructing a drainage channel, so that the drainage and irrigation is ensured to be smooth and unobstructed, the requirement of irrigation can be met in dry seasons, drainage can be timely carried out in rainy seasons, the water accumulation in coal gangue soil experimental fields is prevented, and the drainage is ensured to be smooth and unobstructed especially in heavy rain days.|[0021] (5) According to the method, a large number of shrubs and herbaceous plants are screened, and the results show that amorpha fruticosa, sea buckthorn, kochia scoparia, calliopsis javanica and Festuca arundinacea are obtained, and the plant varieties have high tolerance to coal gangue, can adapt to local ecological environment, and effectively improve the survival rate of the plants.|[0022] (6) The modifier used in the method contains organic fertilizer, so that the fertility of the coal gangue soil is improved, and the silicate bacteria are guaranteed to have enough nutrients to grow and reproduce.|[0023] (7) The modifier can well increase the content of organic matters in the coal gangue and meet the basic requirements of animal and plant growth in soil.|[0024] (8) In the method, the residue of the plant is left in the plant after a life cycle, so that the carbon content in the coal gangue soil is increased, and carbon in the atmosphere can be effectively fixed in the soil.|INVENTION MODE|Detailed Description|[0025] The present invention is further illustrated but not limited in any way by the following description, and any alterations or substitutions based on the teachings of the present invention are intended to fall within the scope of the present invention.|[0026] Example 1: method for realizing soil formation and carbon sequestration by using phosphogypsum and coal gangue|Crushing large-particle coal gangue;|step two, paving the crushed phosphogypsum in a field;|leveling the field to level the surface of the field;|step four, arranging a drainage ditch: the depth of the ditch is 40cm, the width is 50cm, and the foundation is tamped; pouring concrete on two sides of the road, two sides of the drainage ditch and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm above the water level.|[0027] Step five, adding phosphogypsum and a modifier: paving a phosphogypsum layer and a modifier on the surface of the coal gangue layer, wherein the thickness of the paved phosphogypsum is 10cm, the modifier is biological carbon, organic fertilizer and biological straw, and the volume ratio of the modifier to the phosphogypsum layer is 4:2:2, and the paving thickness is 4cm. And after the phosphogypsum layer and the modifier layer are laid, ploughing to uniformly distribute the phosphogypsum and the modifier in the coal gangue layer. Then planting plants, adopting a cultivation method for shrubs, manually digging pits on the ploughed coal gangue according to the density of 1 pit per square meter per sapling, wherein the diameter of each pit is 0.9m, the pit depth is 0.6m, the pits are in a plum blossom shape through cross excavation, purchasing nursery stocks with soil balls, the diameter of each soil ball is not more than 40cm, the height of each soil ball is less than 50cm, the shrubs are amorpha fruticosa and sea buckthorn, and checking whether the nursery stocks are qualified before planting, if the branches are complete, whether the nursery stocks reach the standard. Tamping soil balls after cultivation, finishing the landform, applying 50 g/seedling of Bacillus mucilaginosus in a hole with the depth of 20cm at a position 5cm away from the seedlings, and immediately covering soil after application. Selecting Kochia scoparia, callistephus and Festuca arundinacea for herbaceous plants, sowing the grass seeds at a rate of 15g per square meter, performing spray application of Bacillus mucilaginosus at a rate of 0.5kg per 100 square meters after sowing the grass seeds, and immediately covering dry grass mats after application.|[0028] The organic fertilizer is fermented and decomposed chicken manure sold in the market; the biochar is a powdery biological organic material sold in the market; the straws are common straws and the length of the straws is 2cm.|[0029] Step six, maintenance: in summer, the temperature is high, the evaporation of water on the surface layer of the soil is fast, the growth and development of herbaceous plants are not facilitated, in order to reduce the water loss and the temperature of the surface layer of the soil, dry grass mats are paved on the surface of the soil during the cultivation period of the Kochia scoparia, the Calliopsis and the Festuca arundinacea, wet grass mats with the thickness of 2cm are replaced after the seeds bud, the humidity of the grass mats is kept at 70%, and the grass mats are removed when the seedlings grow to 7 cm. And timely reseeding the planting points with seedling shortage.|[0030] The survival rate of amorpha fruticosa and sea buckthorn can reach 92%, and the survival rate of Kochia scoparia, calliopsis and Festuca arundinacea can reach 96%.|[0031] Example 2:|crushing large-particle coal gangue;|step two, paving the crushed phosphogypsum in a field;|leveling the field to level the surface of the field;|step four, arranging a drainage ditch: the depth of the ditch is 40cm, the width is 50cm, and the foundation is tamped; pouring concrete on two sides of the road, two sides of the drainage ditch and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm higher than the water outlet plane.|[0032] Step five, adding the phosphogypsum and the modifying agent: paving a phosphogypsum layer and a modifier on the surface of the coal gangue layer, wherein the thickness of the paved phosphogypsum is 10cm, the modifier is biological carbon, organic fertilizer and biological straw, and the volume ratio of the modifier to the phosphogypsum layer is 5:2:2, and the paving thickness is 4cm. And after the phosphogypsum layer and the modifier layer are laid, ploughing to uniformly distribute the phosphogypsum and the modifier in the coal gangue layer. Then planting plants, adopting a cultivation method for shrubs, manually digging pits on the ploughed coal gangue according to the density of 1 pit per square meter per sapling, wherein the diameter of each pit is 0.9m, the pit depth is 0.6m, the pits are in a plum blossom shape through cross excavation, purchasing nursery stocks with soil balls, the diameter of each soil ball is not more than 40cm, the height of each soil ball is less than 50cm, the shrubs are amorpha fruticosa and sea buckthorn, and checking whether the nursery stocks are qualified before planting, if the branches are complete, whether the nursery stocks reach the standard. Tamping soil balls after cultivation, finishing the landform, applying 50 g/seedling of Bacillus mucilaginosus in a hole with the depth of 20cm at the position 5cm away from the seedlings, and immediately covering soil after application. The method is characterized in that the Kochia scoparia, the cosmos and the festuca arundinacea are selected for herbaceous plants, the grass seed sowing amount is 15g per square meter, the bacillus mucilaginosus is applied by spraying after the grass seed sowing, the application amount is 0.5kg per 100 square meters, and the grass mat is immediately covered after the application.|[0033] The organic fertilizer is fermented and decomposed chicken manure sold in the market; the biochar is a powdery biological organic material sold in the market; the straws are common straws and the length of the straws is 2cm.|[0034] Step six, maintenance: the temperature is high in summer, the water in the surface layer of the soil is quickly evaporated, the herbaceous plant growth and development are not facilitated, in order to reduce the water loss and the temperature of the surface layer of the soil, during the cultivation period of Kochia scoparia, sphaerotheca persica and Festuca arundinacea, dry grass mats are laid on the surface of the soil, wet grass mats with the thickness of 2cm are replaced after the seeds sprout, the humidity of the grass mats is kept at 70%, and the grass mats are removed when the seedlings grow to 7 cm. And timely reseeding the planting points with seedling shortage.|[0035] The survival rate of amorpha fruticosa and sea buckthorn can reach 93%, and the survival rate of Kochia scoparia, calliopsis and Festuca arundinacea can reach 95%.|[0036] Example 3:|crushing large-particle coal gangue;|step two, paving the crushed phosphogypsum in a field;|leveling the field to level the surface of the field;|step four, arranging a drainage ditch: the depth of the ditch is 40cm, the width is 50cm, and the foundation is tamped; pouring concrete on two sides of the road and two sides and the bottom of the drainage ditch; a plastic partition plate with the thickness of 2cm is placed between the drainage ditch and the road, the total height of the partition plate is 60cm, the downward depth is 20cm, and the height of the partition plate is 40cm above the water level.|[0037] Step five, adding phosphogypsum and a modifier: paving a phosphogypsum layer and a modifier on the surface of the coal gangue layer, wherein the thickness of the paved phosphogypsum is 10cm, and the modifier is biological carbon, organic fertilizer and biological straw according to the volume ratio of 6:2:2, and the paving thickness is 4cm. And after the phosphogypsum layer and the modifier layer are laid, ploughing to uniformly distribute the phosphogypsum and the modifier in the coal gangue layer. Then planting plants, adopting a cultivation method for shrubs, manually digging pits on the ploughed coal gangue according to the density of 1 pit per square meter per sapling, wherein the diameter of each pit is 0.9m, the pit depth is 0.6m, the pits are in a plum blossom shape through cross excavation, purchasing nursery stocks with soil balls, the diameter of each soil ball is not more than 40cm, the height of each soil ball is less than 50cm, the shrubs are amorpha fruticosa and sea buckthorn, and checking whether the nursery stocks are qualified before planting, if the branches are complete, whether the nursery stocks reach the standard. Tamping soil balls after cultivation, finishing the landform, applying 50 g/seedling of Bacillus mucilaginosus in a hole with the depth of 20cm at a position 5cm away from the seedlings, and immediately covering soil after application. The method is characterized in that the Kochia scoparia, the cosmos and the festuca arundinacea are selected for herbaceous plants, the grass seed sowing amount is 15g per square meter, the bacillus mucilaginosus is applied by spraying after the grass seed sowing, the application amount is 0.5kg per 100 square meters, and the grass mat is immediately covered after the application.|[0038] The organic fertilizer is fermented and decomposed chicken manure sold in the market; the biochar is a powdery biological organic material sold in the market; the straws are common straws and the length of the straws is 2cm.|[0039] Step six, maintenance: in summer, the temperature is high, the evaporation of water on the surface layer of the soil is fast, the growth and development of herbaceous plants are not facilitated, in order to reduce the water loss and the temperature of the surface layer of the soil, dry grass mats are paved on the surface of the soil during the cultivation period of the Kochia scoparia, the Calliopsis and the Festuca arundinacea, wet grass mats with the thickness of 2cm are replaced after the seeds bud, the humidity of the grass mats is kept at 70%, and the grass mats are removed when the seedlings grow to 7 cm. And timely replanting the planting points with seedling shortage.|[0040] The survival rate of amorpha fruticosa and sea backthern can reach 91%, and the survival rate of kochia scoparia, cosmos and festuca arundinacea can reach 95%.|[0041] Comparative example 1:|the implementation process steps are the same as those of the embodiment 2, but a phosphogypsum layer is not paved on the surface of the coal gangue, and only the modifying agent is paved. The survival rate of amorpha fruticosa and sea backthern is 71%, and the survival rate of kochia scoparia, cosmos and festuca arundinacea is 83%.|[0042] Comparative example 2:|the procedure was carried out in the same manner as in example 2, except that after the cultivation and sowing, bacillus mucilaginosus was not applied. The survival rate of amorpha fruticosa and sea backthern is 56%, and the survival rate of kochia scoparia, cosmos and festuca arundinacea is 68%.|[0043] Comparative example 3:|the procedure was as in example 2, except that no soil was applied to the shrubs after the application of Bacillus mucilaginosus. After the herbaceous plants are sowed, spraying the bacillus mucilaginosus at the application rate of 0.5kg/100 square meter, and covering a dry grass mat every other day after the application. The survival rate of amorpha fruticosa and sea buckthorn is 66%, and the survival rate of Kochia scoparia, sphaerotheca persica and Festuca arundinacea is 78%.|[0044] The construction method provided by the embodiment of the invention is simple, reasonable in manufacturing cost, rapid in greening time effect, wide in application range and simple in construction, can effectively utilize the coal gangue and the phosphogypsum, realizes waste utilization, can achieve the tree survival rate of 91% and the herbaceous plant survival rate of 95%, can be applied to different coal mine area soil engineering, and has strong popularization and application. Family Number|(103202165)|103202165|Abstract|(CN115517043 A)|The invention discloses a method for soil formation and carbon sequestration by synergy of ardealite and coal gangue . The method comprises the following steps : ( 1 ) crushing coal gangue ; ( 2 ) flattening the coal gangue ; ( 3 ) arranging a drainage ditch ; ( 4 ) adding ardealite and a modifier , and ploughing ; ( 5 ) applying a microbial agent : combining spraying and hole application ; ( 6 ) planting or cultivating plants ; ( 7 ) maintenance and irrigation : keeping soil humidity , and spraying pesticides on the planted trees in time to prevent plant diseases and insect pests from threatening the growth of the trees ; grass felts are laid on herbaceous plants , so that the influence of direct sunlight and high temperature is reduced . The construction method is simple , reasonable in manufacturing cost , rapid in greening aging , wide in application range and easy to construct , coal gangue and ardealite can be effectively utilized , waste utilization is achieved , the survival rate of trees can reach 92% or above , the survival rate of herbaceous plants can reach 96% or above , the method can be applied to soil engineering of different coal mine areas , and the application range is wide . And the method has high generalization performance and applicability . |CPC codes|(CN115517043 A)|A01B - 079/02 |A01G - 017/00/5 |A01G - 020/00 |IPC codes|(CN115517043 A)|A01B - 079/02 |A01G - 017/00 |A01G - 020/00 |Title|(CN115517043 A)|Phosphogypsum and coal gangue cooperated soil formation and carbon sequestration method | Environmental technology|Other special machines A01B-079/02|A01G-017/00/5|A01G-020/00|B09C-001/10|B09C-001/10/5|B09C-2101/00 A01B-079/02|A01G-017/00/5|A01G-020/00|B09C-001/10|B09C-001/10/5|B09C-2101/00 A01B-079/02|A01G-017/00|A01G-020/00|B09C-001/10 A01B-079/02|A01G-017/00|A01G-020/00|B09C-001/10 CN117397553B CN117397553B 108171833 WHO=Examiner SELF=N CN114375797|CN113243279|CN109168391|CN103214300|CN111466279|CN109929561 CN114375797 99742291 WHO=Examiner SELF=N CAT=Y|CN113243279 95640952 WHO=Examiner SELF=N CAT=Y|CN109168391 82990134 WHO=Examiner SELF=N CAT=Y|CN103214300 45710873 WHO=Examiner SELF=N CAT=Y|CN111466279 89994738 WHO=Examiner SELF=Y CAT=A|CN109929561 84975595 WHO=Examiner SELF=N CAT=A CN109168391; CN109929561; CN111466279; CN114375797; CN103214300; CN113243279 PENDING (CN115517043)|PENDING ALIVE (CN115517043)|ALIVE (CN115517043)|LEGAL DETAILS FOR CN115517043|Actual or expected expiration date=2042-09-13|Legal state=ALIVE|Status=PENDING|Event publication date=2022-09-13|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211110693|Application date=2022-09-13|Standardized application number=2022CN-1110693|Event publication date=2022-12-27|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115517043|Publication stage code=A|Publication date=2022-12-27|Standardized publication number=CN115517043|Event publication date=2022-12-27|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-01-13|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN115517043)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoS9Tcai2qh4LVfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=xMVIo5yKsYdjlxdI64ZzqJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN115517043)|CN (CN115517043)|NAME=KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN115517043)|NAME=ZHANG YU;Kunming Tongju Patent Agency Co., Ltd. , REG=53214 (CN115517043)|NAME=HUANG JIANHONG|NAME=SHU JUNYU|NAME=ZHAO YUNGE|NAME=ZUO JIANFEN|NAME=TIAN SENLIN|NAME=HU XUEWEI|NAME=ZHAO QUN|NAME=CUI XIANGFEN 0 1 Titre: (CN115517043)|Phosphogypsum and coal gangue cooperated soil formation and carbon sequestration method Résumé: (CN115517043)|The invention discloses a method for soil formation and carbon sequestration by synergy of ardealite and coal gangue. The method comprises the following steps: (1) crushing coal gangue; (2) flattening the coal gangue; (3) arranging a drainage ditch; (4) adding ardealite and a modifier, and ploughing; (5) applying a microbial agent: combining spraying and hole application; (6) planting or cultivating plants; (7) maintenance and irrigation: keeping soil humidity, and spraying pesticides on the planted trees in time to prevent plant diseases and insect pests from threatening the growth of the trees; grass felts are laid on herbaceous plants, so that the influence of direct sunlight and high temperature is reduced. The construction method is simple, reasonable in manufacturing cost, rapid in greening aging, wide in application range and easy to construct, coal gangue and ardealite can be effectively utilized, waste utilization is achieved, the survival rate of trees can reach 92% or above, the survival rate of herbaceous plants can reach 96% or above, the method can be applied to soil engineering of different coal mine areas, and the application range is wide. And the method has high generalization performance and applicability. 33 Abstract gpt-4o-mini no The article focuses on soil formation and carbon sequestration using coal gangue and ardealite, but does not explicitly mention accelerated weathering or mineral carbonation related to CO₂ capture.
36 GB2304769|GB202304769|GB202320054|GB2320054|WOGB2024/050905 WOGB2024/050905|HK62026117260|BR112025016082|EP24719614 HK40129248|BR112025016082|EP4587163|WO2024/201086 111678262 WO2024/201086 A1 2024-10-03 [WO2024201086]|HK40129248 A 2026-03-06 [HK40129248]|BR112025016082 A0 2025-08-12 [BR112025016082]|EP4587163 A1 2025-07-23 [EP4587163] 2023-03-30|2023-12-27|2024-04-02 2024-04-02|2026-01-05|2024-04-02|2024-04-02 2026-03-06|2025-08-12|2025-07-23|2024-10-03 (EP4587163)|2044-04-02|(WO2024/201086)|2026-09-30|(HK40129248)|2044-04-02|(BR112025016082)|2044-04-02 (EP4587163)|Method of sequestering atmospheric carbon (EP4587163)|This invention relates to carbon sequestration, in particular by enhanced weathering. The methods generally utilise an enzyme, typically carbonic anhydrase. In particular, the invention relates to methods of sequestering atmospheric carbon by applying Carbonic Anhydrase, and optionally rock, to soil or earth. An immobilsied enzyme is also provided, along with the use of that enzyme to sequester atmospheric carbon. Mixtures comprising carbonic anhydrase are also provided, for example carbonic anhydrase mixed with one or more of soil, seed and rock. FABRICNANO (EP4587163)|Fabricnano Limited ([GB])|(WO2024/201086)|FABRICNANO LIMITED ([GB])|(HK40129248)|FABRICNANO LIMITED ([GB])| AARONS GRANT|BURNS JONATHAN|SRINIVASAMURTHY VISHNU (EP4587163)|AARONS, Grant|BURNS, Jonathan|SRINIVASAMURTHY, Vishnu (EP4587163)|Elkington and Fife LLP;Prospect House ([GB])|Reg. Nb: 101770561|(WO2024/201086)|ELKINGTON AND FIFE LLP ([GB])|(HK40129248)|WENPING PATENT & TRADE MARK AGENT LIMITED ([HK]) (WO2024/201086)|It is beneficial if the solid support has a procurement cost of $5 or less per kg and beneficial further still if the solid support has a procurement cost of $1 or less per kg, or $0.5 or less per kg.|Scale is easy, speed has been elusive and comes with costs (e.g. grinding rock to be smaller and faster to react with naturally available carbonic acid, but the level of carbonic acid in soil is relatively low concentration and thus limiting on the rate of carbon sequestration).|Without wishing to be bound by theory, the inventors have found that inoculating an enzyme such as Carbonic Anhydrase onto a plant seed or plant root has many advantages over microbial inoculations, including one or more of:| (WO2024/201086)|1. A method of sequestering atmospheric carbon, comprising the step of applying Carbonic Anhydrase to soil.|29. An enzyme immobilised to a plant or plant seed, optionally wherein the enzyme is carbonic anhydrase.|32. A mixture comprising Carbonic Anhydrase and seed, optionally wherein the Carbonic Anhydrase is immobilised to the seed.|33. A mixture comprising Carbonic Anhydrase and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support.|34. A mixture comprising Carbonic Anhydrase and rock, optionally wherein the Carbonic Anhydrase is immobilised to a solid support.|35. A mixture comprising carbonic anhydrase, rock and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support.|38. A method of applying an enzyme to a plant or plant seed, comprising dipping the plant or plant seed into, or spraying the plant or plant seed with, a liquid comprising the enzyme.| (WO2024/201086)|In particular, the invention relates to methods of sequestering atmospheric carbon by applying Carbonic Anhydrase, and optionally rock, to soil or earth.|This invention relates to carbon sequestration, in particular by enhanced weathering.|This invention relates to carbon sequestration, in particular by enhanced weathering. In particular, the invention relates to methods of sequestering atmospheric carbon by applying Carbonic Anhydrase, and optionally rock, to soil or earth.| (EP4587163)|ATMOSPHERIC CARBON(100,1)||(WO2024/201086)|CARBONIC ANHYDRASE(100,219)|ENZYME(100,195)|PLANT(100,53)|SEED(100,53)|ATMOSPHERIC CARBON(100,16)|APPLYING CARBONIC ANHYDRASE(64,4)|PROCUREMENT COST(57,12)|MICROBIAL INOCULATION(56,1)|BOVINE ERYTHROCYTE CARBONIC ANHYDRASE(51,3)|GROUND(49,135)|IMMOBILSIED ENZYME(43,1)|ANIMAL CARBONIC ANHYDRASE(42,6)|GRINDING STONE(42,1)|ROCK(40,112)|VIABLE PLANT SEED(39,1)|PLANT SEED(35,4)|ZETA CARBONIC ANHYDRASE(34,3)|VEGETABLE CROP(32,1)|BACTERIAL CARBONIC ANHYDRASE(31,3)|SHRUB SPECIES(30,1)|CARBON SEQUESTRATION(29,18)|AGRICULTURAL CROP SPECIES(29,1)|PLANT CARBONIC ANHYDRASE(28,3)|PASTURE LAND(28,2)|AMINE FUNCTIONALIZED BEAD(25,7)|SPHERICAL BEAD(21,17)|SPERMATOPHYTE(21,1)|SOLID SUPPORT(20,70)|ENHANCED WEATHERING(20,23)|ADSORBENT BEAD(20,10)|TURNIP CABBAGE(20,1)|PARTICULATE(19,29)|DIPPING(19,2)|OILSEED RAPE(19,1)|PLANT ROOT(18,21)|AGRICULTURAL LAND(18,10)|NONFUNCTIONALISED RESIN BEAD(18,5)|NONCOVALENT(17,3)|NATURALLY AVAILABLE CARBONIC ACID(17,1)|PORE DIAMETER(16,27)|AMINE FUNCTIONALIZED RESIN(16,5)|SWEET POTATO(16,1)|PERFECT BEAD(15,9)|AGRICULTURALLY ACCEPTABLE EXCIPIENT(15,3)|PULVERIZATION(15,3)|SPRAY BAR(15,3)|CARBON SEQUESTRATION RATE(15,2)|ALFALFA(15,1)|CARROT(15,1)|LETTUCE(15,1)|MILLET(15,1)|SORGHUM(15,1)|CARBONIC ACID(14,8)|ANIMAL MATTER(14,4)|MILK PASTEURIZATION(14,4)|REMIN BASALT(14,4)|BROWNFIELD LAND(14,3)|DENTILLAND BASALT(14,3)|DUNTILLAND BASALT(14,3)|SAINSBURY STEAK(14,3)|BROADCAST SPREADER(14,2)|CARBONIC ACID LEVEL(14,1)|MAIZE(13,1)|NITROGEN ADSORPTION(12,9)|CORN HUSK(12,6)|ADSORBENT RESIN BEAD(12,3)|AGRICULTURALLY ACCEPTABLE ADDITIVE(12,3)|ARABLE LAND(12,3)|CRUSHING(12,3)|SHAKING INCUBATOR(12,3)|BEET(12,1)|CALCIMETER DURAN BOTTLE(12,1)|CARBONIC ANHYDRASE REVIEW IMMOBILIZATION(12,1)|POLYMETHACRYLIC DIVINYLBENZENE MACROPOROUS BEAD(12,1)|CARBONIC ANHYDRASE RESULT(11,2)|CONCENTRATED HCI PL(11,2)|FOGL BENCH TOPSOIL(11,1)|RYE(11,1)|SEEDLING ROOT INOCULANT(11,1)|SOY(11,1)|ACRE(10,11)|HECTARE(10,10)|BARLEY(10,4)|BOVINE BLOOD(10,4)|EPOXY BEAD(10,4)|CEREAL PLANT(10,3)|GRASS(10,3)|OCTADECYL METHACRYLATE BEAD(10,3)|BIOINFORMATIC DATABASE(10,2)|BUFFER ACTIVITY KINETIC PLOT(10,2)|MAGNESIUM CARBONATE(10,2)|MAMMALIAN CARBONIC ANHYDRASE(10,2)|ACCELERATED ENZYME LONGEVITY(10,1)|GENUS TRITICUM SPECIES(10,1)|IONIC POLYPEPTIDE IMMOBILIZATION(10,1)|NON HUMAN ANIMAL BLOOD(10,1)|DUST(9,4)|AGRICULTURAL EQUIPMENT(9,3)|BALL MILLING(9,3)|BASALT CARRIER(9,3)|BOVINE SERUM(9,3)|COVALENT BOND(9,3)|PLANT STEM(9,3)|WASTE LAND(9,3)|HOMOLOG IDENTIFICATION(9,2)|CARBONIC ANHYDRASE IMMOBILIZATION(9,1)|LACTICASEIBACILLUS CASEI(9,1)|PEPTIDE GENETIC FUSION(9,1)|PROTEIN IMMOBILIZATION CONTEXT(9,1)|CALCIUM CARBONATE(8,5)|BUTYL METHACRYLATE BEAD(8,4)|COMMERCIAL CROP PLANT(8,4)|PHYSICAL ADSORPTION(8,4)|SEED COATING(8,4)|BAKER YEAST(8,2)|BREWER YEAST(8,2)|EPOXY FUNCTIONALIZED BEAD(8,2)|PLANT BIOMASS(8,2)|PROFILE NORMALIZATION(8,2)|TOPSOIL DEPTH(8,2)|ACCELERATE ADVANCED WEATHERING(8,1)|CAMELLIA SINENSIS(8,1)|DEGTJAREFF EXAMINATION(8,1)|ENTEROCOCCUS BACTERIA(8,1)|GAMMA CARBONIC ANHYDRASE ENZYME(8,1)|GOSSYPIUM ARBORETUM(8,1)|INSTRUMENT HCI CONTAINER(8,1)|MONOATOMIC DICATION(8,1)|MOR BIOINFORMATIC(8,1)|SACCHARMOCYES CEREVISIAE(8,1)|STEAK BLOOD UL(8,1)|TUBER PERIDERM(8,1)|AMBIENT CO2(7,3)|BEAD TOTAL MOISTURE(7,3)|EPOXY FUNCTIONALIZED RESIN(7,3)|PORE VOLUME(7,3)|PRODUCT TITER(7,3)|SEQUESTERING CARBON(7,3)|VIABILITY(7,3)|ACCELERATE ENHANCED WEATHERING(7,2)|FIBROUS MATTER(7,2)|FOLIAR SPRAY(7,2)|POLYPEPTIDE SEQUENCE(7,2)|PROCESSED BASALT(7,2)|ROOT DIP(7,2)|SPRAYED PLANT(7,2)|STRUCTURAL MODIFICATION(7,2)|UNTREATED PLANT(7,2)|UNTREATED SOIL(7,2)|WET SIEVING(7,2)|ACCELERATE NATURAL WEATHERING(7,1)|AGRICULTURAL SOILS(7,1)|AGRONOMIC IMPORTANCE CROP PLANT(7,1)|BILLION TONNE(7,1)|BULB TUNIC(7,1)|CARBONIC ANHYDRASE CLASS(7,1)|CARBONIC ANHYDRASE ENGINEERING(7,1)|CARBONIC ANHYDRASE PROTEIN(7,1)|COMPOST STARTER(7,1)|CRYOPHILIC ORGANISM(7,1)|EN WIKI(7,1)|ENZYME INOCULATED TREE ROOT(7,1)|EPOXY METHACRYLATE BEAD(7,1)|EXPRESS CARBONIC ANHYDRASE(7,1)|FERTILIZING SLURRY(7,1)|GEOLOGY BASALT(7,1)|MESOPHILIC ORGANISM(7,1)|MICROBE EXPRESS(7,1)|NUTRITION ENHANCER(7,1)|POLYMETHACRYLIC DIVINYLBENZENE BEAD(7,1)|RAW GOAT MILK(7,1)|ROCK PARTICLE SIZE DIAMETER(7,1)|ROCK PARTICLE SIZING(7,1)|SIGMA CARBONIC ANHYDRASE(7,1)|SPECIES TRITICUM AESTIVUM(7,1)|STATED CRUDE ENZYME PL(7,1)|TOPSOIL RETENTION(7,1)|FALCON TUBE(6,10)|METAL ION(6,8)|PELLET(6,5)|CO2 SEQUESTRATION(6,4)|DOLOMITE(6,4)|FUME HOOD(6,4)|PLANTING(6,4)|SEAWATER(6,4)|FIBROUS MATERIAL(6,3)|ACCELERATE CO2 CONVERSION(6,1)|ACCELERATED WEATHERING(6,1)|AGRICULTURAL BEAD(6,1)|AGRICULTURAL CROP SEED(6,1)|ANCIENT ENZYME(6,1)|BETA CARBONIC ANHYDRASE(6,1)|BIOMASS DECOMPOSITION(6,1)|BUOYANT BEAD(6,1)|CHICKEN SERUM(6,1)|CO2 CAPTURE(6,1)|CONTROLLABLE PROMOTER(6,1)|COVALENT AMIDE BOND(6,1)|DELTA CARBONIC ANHYDRASE(6,1)|DENATURE MAJORITY(6,1)|EXTREMOPHILE HOST ORGANISM(6,1)|FUSION GENE(6,1)|HARVESTED HORTICULTURAL PRODUCT(6,1)|HOMOLOG SELECTION(6,1)|HOMOLOGOUS ENZYME(6,1)|MULTIMERIC ENZYME(6,1)|OLIVINE ROCK(6,1)|PLANTED CROP(6,1)|RECOMBINANT ENZYME(6,1)|RELEVANT BEAD SCREEN(6,1)|SOIL DRENCH(6,1)|SUPERNATANT PL(6,1)|TURNOVER CO2(6,1)|UL SUPERNATANT(6,1)|AVERAGE PARTICLE SIZE(5,25)|GROUND SURFACE(5,12)|SHORT SPACER(5,8)|OPTIMUM TEMPERATURE(5,7)|BICARBONATE(5,3)|CARBONATE CONTENT(5,3)|DRY ICE FUME(5,3)|MACHINERY(5,3)|PRODUCTIVITY(5,3)|PROTEASE(5,3)|SEARCH OUTPUT(5,3)|VERMICULITE(5,3)|CARBON SELL(5,2)|CONVERT CO2(5,2)|DEACTIVATION MODE(5,2)|DRY SIEVING(5,2)|EXPERIMENTALIST(5,2)|RESIDUAL BLOOD(5,2)|SHOW ACTIVITY KINETIC PLOT(5,2)|WASH CENTRIFUGATION CYCLE(5,2)|ABSORBANCE PROFILE(5,1)|ACCELERATED ENHANCED WEATHERING(5,1)|AGRONOMIC BENEFIT(5,1)|ALMOST QUANTITATIVE LOADING(5,1)|ALPHA CARBONIC ANHYDRASE(5,1)|AMBIENT SURROUNDINGS(5,1)|BASALT PARTICLE(5,1)|BROADCASTER EQUIPMENT PIECE(5,1)|CARBONIC ANHYDRASE PERFORMANCE(5,1)|CHARGED CATION(5,1)|CLASSICAL LITERATURE SEARCH(5,1)|CO2 EMISSION(5,1)|COMPATIBLE CROP(5,1)|COMPLEX POLYSACCHARIDE(5,1)|COVALENT LINKAGE(5,1)|CRAG MILL(5,1)|CROP ABSENCE(5,1)|DNA ENZYME(5,1)|ENZYME INOCULATED SEED(5,1)|ENZYME PACKING(5,1)|ENZYME SLURRY(5,1)|EXPRESSION VESSEL(5,1)|FAST SOIL HEALTH RECOVERY(5,1)|FIBROUS PLANT(5,1)|GROCERY STORE STEAK(5,1)|HUMAN CARBONIC ANHYDRASE(5,1)|HYBRID CATALYST(5,1)|IIIPAC NAME(5,1)|IMMOBILIZATION SOIL TEST(5,1)|IMPARTING STABILITY(5,1)|INERT SUBSTANCE(5,1)|LECO ANALYSIS(5,1)|LINKED ENZYME(5,1)|MAMMALIAN TISSUE(5,1)|MATURE PLANT(5,1)|MICROALGAE CELL(5,1)|MICROBIAL GROWTH PATTERN(5,1)|NATURAL RAINFALL(5,1)|PARTLY PURIFIED CARBONIC ANHYDRASE(5,1)|PDB ENTRY(5,1)|PEPTIDE CATALYST(5,1)|PLANT TUBEROUS ROOT(5,1)|POLYSTYRENE BEAD(5,1)|PRESSING TART(5,1)|PROLONGED PROXIMITY(5,1)|REACTING CARBONIC ANHYDRASE(5,1)|RECOMBINANT EXPRESSION CASSETTE(5,1)|SEED PRIMING(5,1)|SILICATE ROCK(5,1)|UL PCR TUBE(5,1)|SILICA GEL(4,17)|DDH2O(4,5)|SEQUENCE SIMILARITY(4,4)|SEQUESTER CARBON(4,4)|AGRICULTURE(4,2)|BUBBLING(4,2)|FLUCTUATION(4,2)|FUNGUS(4,2)|MICROBIAL INOCULANT(4,2)|MUTATION(4,2)|NIGHT AVERAGE TEMPERATURE(4,2)|PERLITE(4,2)|SACCHARUM(4,2)|SHAKER(4,2)|SOIL ACIDIFICATION(4,2)|SPRAYING(4,2)|STATED REACTION(4,2)|WASTE MATTER(4,2)|WATERING(4,2)|YOGURT(4,2)|ACCELERATE ABILITY(4,1)|ACTINOMYCETE(4,1)|ACTIVE ENTITY(4,1)|ACTIVITY ASSAY(4,1)|AGGREGATE STABILITY(4,1)|AGRICULTURALLY ACCEPTABLE SOLID CARRIER(4,1)|ARCHAEA CELL(4,1)|ATMOSPHERIC CARBON DIOXIDE FIXING(4,1)|BACTERIAL CELL(4,1)|BASALT MASS(4,1)|BASALT SOURCE(4,1)|BLOOD SOLUTION PL(4,1)|BOEHMERIA NIVEA(4,1)|BUBBLE FORMATION(4,1)|BUFFER REAGENT(4,1)|BUFFERED REACTION(4,1)|CACO3 EQUIVALENT(4,1)|CARBON SEQUESTRATION PROJECT(4,1)|CARBONIC ANHYDRASE REMAINS(4,1)|CHROMIC ACID TITRATION(4,1)|COATING ROCK(4,1)|COFACTOR(4,1)|CORCHORUS CAPSULARIS(4,1)|CROP PLANT SEED(4,1)|DRY COMBUSTION(4,1)|ECONOMICALLY EFFICIENT DOSAGE(4,1)|ELEMENTAL TEST(4,1)|ENHANCED WEATHERING PROJECT(4,1)|FUTURE TEMPERATURE PREDICTION(4,1)|GOSSYPIUM BARBADENSE(4,1)|GOSSYPIUM HERBACEUM(4,1)|GOSSYPIUM HIRSUTUM(4,1)|HORDEUM VULGARE(4,1)|IMMOBILIZATION SUPPORT(4,1)|KEY FINDING(4,1)|LOLIUM MULTIFLORUM(4,1)|MEASURING SOIL RESPIRATION(4,1)|MICROBIAL CELL(4,1)|MINERAL EARTH(4,1)|MINUS COATING(4,1)|NANOPARTICLE NANOMATERIAL(4,1)|NATURAL ENZYME(4,1)|NICOTIANA TABACUM(4,1)|OFF BASALT ROCK(4,1)|PBS BUFFER(4,1)|PH REGULATOR(4,1)|PL PLOT(4,1)|PLANT SPECIES(4,1)|PROLONGED CARBON(4,1)|RESIDUE REACTION(4,1)|ROCKY SOIL(4,1)|SAMPLE CO2 EQUIVALENT(4,1)|SCALE INTERSECTION(4,1)|SCHIZOSACCHAROMYCES POMBE(4,1)|SOLID CARBONATE MINERAL(4,1)|SPECTROPHOTOMETRIC OPTICAL DENSITY READOUT(4,1)|STEEL SLAG(4,1)|SYNTHETIC ORIGIN(4,1)|TIMESCALE(4,1)|TOPSOIL PLANT ORGANIC MATTER(4,1)|UNPASTEURIZED(4,1)|WASTE CELLULOSE(4,1)|YEARLY AVERAGE(4,1)|CACI(3,3)|CHEMISTRY(3,3)|ENZYMATIC ACTIVITY(3,3)|ENZYME REACTION(3,3)|PROTON(3,3)|SERIAL DILUTION(3,3)|SLOPE(3,3)|RECORDING TEMPERATURE(3,2)|ACIDIC CONDITION(3,1)|ADDRESS ANTHROPOGENIC CLIMATE CHANGE(3,1)|ALGINATE(3,1)|AMINE RESIN(3,1)|AUTHOR(3,1)|BIOINFORMATICS TOOL UTILITY(3,1)|BLOOD RATIO(3,1)|BOOST CARBON DIOXIDE(3,1)|BOULDER(3,1)|BRASSICA JUNCEA(3,1)|BRASSICA NAPUS(3,1)|BRASSICA RAPA(3,1)|CANNABIS SATIVA(3,1)|CARBON CREDIT DURATION(3,1)|CARBONATE FORMATION(3,1)|CAROTENOID(3,1)|CHANGING PH(3,1)|CHEMOSPHERE(3,1)|CHIMNEY(3,1)|CHURNING(3,1)|COFFEA ARABICA(3,1)|COFFEA ROBUSTA(3,1)|COLD GEOGRAPHICAL LOCATION(3,1)|COLLOID(3,1)|COLOR CHANGE(3,1)|CONVERSION MEASUREMENT(3,1)|COW RED BLOOD CELL(3,1)|CROP PLANT YIELD(3,1)|DEACTIVATION PREVENTION(3,1)|DEAD PLANT MATTER(3,1)|DEPLETION(3,1)|DIMERIC(3,1)|DRIED POWDER(3,1)|ENHANCED WEATHERING ENVIRONMENT(3,1)|ENZYME ACTIVITY RETENTION(3,1)|ENZYME CATALYSIS(3,1)|ENZYME LIQUID(3,1)| (WO2024/201086)|Claims |1. A method of sequestering atmospheric carbon, comprising the step of applying Carbonic Anhydrase to soil.|2. A method according claim 1, wherein the step of applying the Carbonic Anhydrase to the soil compromises applying the Carbonic Anhydrase and rock to the soil.|3. The method of claim 1 or claim 2, wherein the Carbonic Anhydrase is immobilised to a solid support.|4. The method of claim 3, wherein the solid support comprises or consists of: plant matter, optionally wherein the plant matter comprises or consists of corn husks and/or cellulose; and/or animal matter; and/or fibrous materials; and/or a bead; optionally wherein the solid support comprises or consists of waste material.|5. The method of claim 3 or claim 4, wherein the solid support comprises or consists of a plant seed, optionally a viable plant seed.|6. The method of claim 5, wherein the Carbonic Anhydrase is immobilised to the seed coat, optionally wherein the immobilisation is carried out by spraying the seed with, or dipping the seed into, or otherwise coating the seed with, a liquid comprising the carbonic anhydrase.|7. The method of claim 6, wherein the solid support is immobilised to the seed coat before seed priming, during seed priming, or after seed priming.|8. The method of any of claims 5 to 7, wherein the seed is an agricultural crop species, optionally selected from: a cereal, corn, barley, wheat, maize, millet, oats, rye, rice or sorghum; a pulse- or bean-species such as soy; or a vegetable crop such as potato, beet, carrot, sweet potato, turnip cabbage or lettuce.|9. The method of any of claims 5 to 7, wherein the seed is cotton, alfalfa, oilseed rape or a grass.|10. The method of any of claims 5 to 7, wherein the seed is a tree or shrub species.|11. The method of claim 3 or claim 4, wherein the solid support comprises or consists of a plant, optionally a spermatophyte, optionally as defined in any of claims 8 to 10.|12. The method of claim 11 , wherein the Carbonic Anhydrase is immobilised to the plant stem and/or plant root, typically the plant root optionally prior to contacting the root with the soil.|13. The method of any of claims 3 to 9, wherein the solid support has a procurement cost of $20 or less per kg, $10 or less per kg, $5 or less per kg, $1 or less per kg, or $0.5 or less per kg.|14. The method of claim 2, wherein the Carbonic Anhydrase is immobilised to the rock, optionally directly to the rock, optionally by covalent bond or by non-covalent means such as physical adsorption.|15. The method of any preceding claim, wherein: the Carbonic Anhydrase has a structural modification to the enzyme which is intended to increase retention at a specified depth and/or location in or on the soil, and/or the Carbonic Anhydrase is provided in a mixture, formulation or composition which is intended to increase retention at a specified depth and/or location in or on the soil.|16. The method of any preceding claim, wherein the Carbonic Anhydrase is retained in or on top soil; optionally wherein the top soil extends 1 metre or less from the soil surface, optionally 50 centimetres or less, 30 centimetres or less, 25 centimetres or less, 20 centimetres or less, 15 centimetres or less, or 10 centimetres or less.|17. The method of any preceding claim, wherein the Carbonic Anhydrase is substantially retained at or around the roots of a plant, optionally in contact with one or more roots.|18. The method of any preceding claim, wherein|(i) the soil is within: agricultural land, optionally wherein the agricultural land is arable land or pasture land; waste land; brownfield land; or industrial land; and/or|(ii) the applying step comprises spraying the Carbonic Anhydrase onto the soil, optionally wherein the Carbonic Anhydrase is present in a slurry when sprayed, optionally wherein the slurry comprises rock, and optionally wherein the slurry is sprayed using agricultural equipment for example a spray bar or broadcast spreader; and/or |(iii) the content of carbon retained in the soil increases as a result of the Carbonic Anhydrase having been applied to the soil. |19. The method of any of claims 2 to 18, wherein the Carbonic Anhydrase and rock are applied to the soil simultaneously, contemporaneously or at different times.|20. The method of any of claims 2 to 19, wherein the rock is a source of metal ions; optionally wherein the metal ions are cations, optionally wherein the cations are any of Mg+2 or Ca+2.|21. The method of any of claims 2 to 20, wherein: the rock comprises silica, optionally wherein the rock comprising silica is basalt or olivine; and/or the rock is particulate, optionally having a particle size diameter of 5 millimetres of less, or 4 millimetres or less, and/or having a 500 micrometres or greater, optionally wherein the rock particle size diameter is about 500 micrometres to about 10 millimetres, or is about 500 micrometres to about 4000 micrometres, or is about 500 micrometres to about 2000 micrometres.|22. The method of any of claims 2 to 21 , wherein the method comprises the step of reducing the rock in size before application to the soil, optionally wherein the rock is reduced in size by crushing, grinding, sieving, milling, pulverisation, and/or ball milling.|23. The method of any of claims 2 to 22, wherein the rock is applied to the soil as a dust, powder, or particulate.|24. The method of any preceding claim, wherein the Carbonic Anhydrase comprises an animal carbonic anhydrase, a plant carbonic anhydrase, and/or a bacterial carbonic anhydrase; optionally wherein the animal Carbonic Anhydrase comprises bovine erythrocyte carbonic anhydrase; optionally wherein the carbonic anhydrase is within a cell when it is applied to the soil.|25. The method of any preceding claim, wherein the Carbonic Anhydrase comprises an alpha, beta, delta, gamma, or zeta carbonic anhydrase.|26. The method of any preceding claim, wherein the Carbonic Anhydrase is mesophilic or cryophilic.|27. The method of any preceding claim, wherein the atmospheric carbon is sequestered as a carbonate, optionally as a magnesium carbonate or a calcium carbonate.|28. A sequestered carbon quantity obtained or obtainable by the method of any of claims 1 - 27.|29. An enzyme immobilised to a plant or plant seed, optionally wherein the enzyme is carbonic anhydrase.|30. An enzyme immobilised to a plant according to claim 29, wherein: the enzyme is mammalian; and/or the enzyme is obtained from non-human animal blood; and/or the enzyme is obtained from bovine or ovine blood; and/or the enzyme is immobilised to the plant root.|31. Use of the Carbonic Anhydrase according to claim 29 or 30 to sequester atmospheric carbon.|32. A mixture comprising Carbonic Anhydrase and seed, optionally wherein the Carbonic Anhydrase is immobilised to the seed.|33. A mixture comprising Carbonic Anhydrase and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support.|34. A mixture comprising Carbonic Anhydrase and rock, optionally wherein the Carbonic Anhydrase is immobilised to a solid support.|35. A mixture comprising carbonic anhydrase, rock and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support.|36. Use of a mixture according to any of claims 32 - 35 to sequester atmospheric carbon.|37. A mixture according to any of claims 32 - 35, for use in sequestering atmospheric carbon.|38. A method of applying an enzyme to a plant or plant seed, comprising dipping the plant or plant seed into, or spraying the plant or plant seed with, a liquid comprising the enzyme.|39. A method according to claim 38, wherein the enzyme is carbonic anhydrase. (WO2024/201086)|[0001] METHOD OF SEQUESTERING ATMOSPHERIC CARBON | [0002] Field of the Invention | [0003] This invention relates to carbon sequestration, in particular by enhanced weathering. In particular, the invention relates to methods of sequestering atmospheric carbon by applying Carbonic Anhydrase, and optionally rock, to soil or earth. | [0004] Background of the Invention | [0005] Enhanced weathering sequesters carbon from carbon dioxide, accelerating the natural process of rock weathering. The application of finely-ground rock to agricultural land is one known method of utilising enhanced weathering to sequester atmospheric carbon. de Oliveira Maciel et al. (Chemosphere, July 2022, 299, 134419, 1-25) review the use of Carbonic Anhydrase to boost carbon dioxide sequestration. The authors note that Carbonic Anhydrase can be utilised in accelerated weathering. Ren et al. (Colloids and Surfaces B: Bioterfaces, August 2021 , 204, 111779, 1-10) review immobilisation of Carbonic Anhydrase and note the high cost of immobilisation supports. | [0006] There remains a need to improve methods of carbon sequestration, to address anthropogenic climate change and increase food security. | [0007] Summary of the Invention | [0008] The present disclosure relates in general to methods of carbon sequestration by enhanced weathering. The methods generally utilise an enzyme, typically carbonic anhydrase. In particular, the methods relate to application of an enzyme (such as carbonic anhydrase) and rock to soil, earth or ground. The methods also relate to contacting a plant or plant seed with Carbonic Anhydrase and then contacting that enzyme-inoculated plant material with the soil, i.e. by planting the seed or plant into the soil. Typically, this is carried out at large scale such a planting one or more fields with enzyme-inoculated seeds or plant material, or re-foresting an area with enzyme-inoculated tree roots. | [0009] This application of enzyme to a typically large area differs from “smokestack” carbon sequestration where carbon dioxide is removed from a chimney and where enzyme re-use and recycling is typically required. | [0010] The enzyme may be any enzyme that is capable of enhancing carbon sequestration into soil. The enzyme may be any enzyme that is capable of increasing plant yield.The enzyme may be any enzyme that is capable of capturing ambient carbon dioxide. | [0011] The enzyme is typically a carbonic anhydrase. Carbonic anhydrases are enzymes that convert carbon dioxide and water into bicarbonate and protons. | [0012] Enhanced weathering aims to accelerate the natural weathering of rock by spreading finely ground silicate rock, such as basalt, onto surfaces which speeds up chemical reactions between rocks, water, and air. It removes carbon dioxide (CO2) from the atmosphere, permanently storing it in solid carbonate minerals. | [0013] Enhanced weathering technology typically uses rock. This could include Olivine rock, Basalt, and other rocks rich in metal ions. The rock may be particulate. | [0014] Enhanced weathering projects have recently had MRV (Measurement Reporting, Verification) models accepted for carbon credits that can be sold commercially. Carbon credits are typically sold as carbon stored on a 20 year horizon. The MRV model is built around these timescales. Carbon sold at this price is currently charged at $200/ton of carbon sequestered from the ambient air. | [0015] Carbon credit duration can be securitized such that 1 year carbon sells for $800/ton and 20 year carbon sells for up to $200/ton. These prices come from present day demand shocks/high levels always being greater than prolonged carbon purchasing. If carbon sequestration projects could be accelerated than the total value from any project would be multiplied by 2x, 3x, 4x, or more. | [0016] Carbonic anhydrase is an enzyme that is widely known to produce carbonic acid from ambient CO2 and H2O. Carbonic Anhydrase is readily available at scale, studied extensively because of its prominence in natural systems as a pH regulator, and many commercial projects exist to try and sequester carbon using this enzyme. | [0017] Carbonic anhydrase can sometimes be very stable, but this depends on the host organism and enzymes from extremophile host organisms typically exhibit the highest stability to prolonged and continuous deactivation modes. | [0018] The Carbonic Anhydrase is typically immobilised to a solid support. The solid support may comprise or consist of rock, for example particulate rock such as basalt particles. The solid support may be a solid support that is separate from the rock, and which can be mixed with the rock. | [0019] In some embodiments, the solid support can be the rock, for example the particulate rock or rock sand. Accordingly, the disclosure provides immobilizing directly onto the ground rocks, e.g. finely ground rocks, via any binding chemistry and/or interaction. In some embodiments,the Carbonic Anhydrase is immobilised to the rock, optionally directly to the rock, optionally by covalent bond or by non-covalent means such as physical adsorption. | [0020] In some embodiments, cheap materials are used as the solid support for immobilisation to ensure commercial viability (e.g. waste solid supports and materials <$10, beneficially <$5, further beneficially <$1 kg, further beneficially <$0.5/kg). Examples of such materials include corn husks, waste cellulose, waste fibrous materials, typically farming additives used for liming such as vermiculite. | [0021] In some embodiments, the solid support is a plant seed. | [0022] In some embodiments the disclosure provides soil + finely ground rock + enzyme +/- immobilization. | [0023] In some embodiments the Carbonic Anhydrase enzyme is not immobilised, i.e. is a “free” enzyme. In some embodiments, the free enzyme binds to plant roots in the top soil or plant material above the top soil. | [0024] In some embodiments, the Carbonic Anhydrase enzyme is designed or engineered to accomplish retention at a specified soil depth with or without immobilisation, for example artificially making larger enzyme radius of gyration, and/or making enzyme charged so that it binds to plant roots at the optimal depth where CO2 is typically present at the roots. Accordingly, in some embodiments, the Carbonic Anhydrase enzyme is immobilised to the plant root. | [0025] Carbon can be introduced into the soil by the fixing of atmospheric carbon dioxide into plant biomass. The carbon in the plant biomass may then be converted into carbon dioxide by the respiration of organisms that aid the decomposition of the dead plant matter. Therefore, immobilising the enzyme to the plant root may be particularly beneficial, as this may bring the Carbonic Anhydrase enzyme in closer proximity to the organisms that aid the decomposition of the dead plant. In some embodiments, therefore, the solid support is a plant root or other part of a plant. | [0026] Carbon sequestration via enhanced weathering technology is readily scalable and almost profitable, but too slow to be economically attractive and impactful. The entire commercial value of enhanced weathering lies at the intersection of scale and speed. Scale is easy, speed has been elusive and comes with costs (e.g. grinding rock to be smaller and faster to react with naturally available carbonic acid, but the level of carbonic acid in soil is relatively low concentration and thus limiting on the rate of carbon sequestration). | [0027] In some embodiments, an increase in soil organic carbon comprises an increase in the level of stable carbon in the soil.In some embodiments, an increase in soil organic carbon comprises an increase in aggregate stability of the soil. | [0028] Typically, the “finely” ground rock particle sizes used in enhanced weathering are on the order of greater than 1 mm or even greater than 10 mm in diameter whereas enzymes are on the order of less than 10 nm in diameter. Enzymes are therefore much smaller, and as in reactor design around immobilized enzymes, this means that the enzyme is likely to leave the reaction environment before any chemical production is accomplished. | [0029] In some embodiments, the rock is particulate and has an average particle size of 50 micrometres or more, more typically 300 micrometres or more for example 500 micrometres or more. In some embodiments, the rock is particulate and has an average particle size of 5 millimetres or less. In some embodiments, the rock is particulate and has an average particle size of 4 millimetres or less. In some embodiments, the rock is particulate and has an average particle size of about 500 micrometres to about 5 millimetres micrometres. In some embodiments, the rock is particulate and has an average particle size of about 50 micrometres to about 4000 micrometres. In some embodiments, the rock is particulate and has an average particle size of about 500 micrometres to about 4000 micrometres. In some embodiments, the rock is particulate and has an average particle size of about 500 micrometres to about 2000 micrometres, or about 500 micrometres to about 1500 micrometres, or about 500 micrometres to about 1000 micrometres, or about 500 micrometres to about 750 micrometres. In some embodiments, the rock is particulate and has an average particle size of about 1 millimetre to about 4 millimetres, or about 2 millimetres to about 4 millimetres, or about 750 micrometres to about 4 millimetres, or about 750 micrometres to about 4.5 millimetres. In all of these embodiments, a typical rock is basalt. | [0030] In an improved method of enhanced weathering described herein, the enzyme stays close to the finely ground rock to help accelerate the carbon sequestration through local carbonic acid formation. The disclosed methods and compositions therefore resist the enzyme from being pushed deeper and deeper into the soil. | [0031] Enhanced weathering works effectively when ambient CO2 is brought down to the soil (or ground, or earth) by natural rainfall, although this could be extended artificially through techniques such as irrigation fields. When it rains and H2O brings CO2 to the Carbonic Anhydrase enzyme, carbonic acid forms, but also the enzyme tends to leach deeper into the soil because the enzyme is much smaller than the soil particle size and enzyme packing/residence time in the soil amongst the finely ground rock is vanishingly short. Thisdrives the whole application of enzymes to the enhanced weathering process to be technoeconomically unviable. | [0032] By increasing the surface area and particle size of the enzyme through immobilization onto a solid support biocatalyst, then the enzyme can be applied in economically efficient dosage to any enhanced weathering process and accelerate the carbon sequestration through prolonged proximity to the finely ground rock with charged metal ions. | [0033] Methods of the present invention are particularly advantageous as they utilise Carbonic Anhydrase in enhanced weathering applications to accelerate the ability of finely ground rocks to sequester carbon. The application of enzymes to finely ground rock for the purpose of enhanced weathering and carbon sequestration is beneficial. Advantageously, methods of the present invention bring about faster climate change impact from the same footprint and faster soil health recovery. Soil health may comprise increasing levels of organic soil matter, changing pH, and/or changing microbial growth patterns. | [0034] Certain aspects of the invention comprise one or more, for example all, of the following features: | [0035] 1 . An enzyme is selected to improve the enhanced weathering technology (in one of many technical and commercial ways). a. Specifically, the Carbonic Anhydrase enzyme rapidly accelerates the formation of carbonic acid in the soil and this is rapidly interacted with metal ions, optionally provided by the finely ground rock to accelerate the overall enhanced weathering. The metal ions may already be present in the soil. | [0036] 2. A solid support or solid support material may be selected for compatibility with the end field of use. The solid support may be a seed or a plant, or a rock. | [0037] 3. A binding chemistry or interaction is chosen for linking the enzyme to the solid support or solid support material. This can also selected for compatibility with the end field of use.| [0038] 4. The enzyme may be immobilized on the solid support or solid support material before application to the field of use. | [0039] 5. The enzyme can be pre-selected for compatibility with the solid support or solid support material and binding chemistry and/or interaction chosen. | [0040] 6. The immobilized enzyme is stabilized to prolonged continuous deactivation modes typically experienced for free enzymes (e.g. thermal).7. The immobilized enzyme is shielded from any deactivation and/or degradation due to protease activity because it is fastened to a much larger entity and restricting the protease from acting on the enzyme of interest. | [0041] 8. The immobilized enzyme is retained in the top soil being exposed to enhanced weathering technology (e.g. finely ground rock) due to the physical properties of the solid support (e.g. larger geometric size, charge, density) | [0042] 9. The solid support or solid support material is chosen to improve the top soil retention of the immobilized enzyme. | [0043] 10. The solid support or solid support material is chosen to promote the immobilized enzyme concentration/presence at a specified depth in the soil (e.g. might be nearer the roots of the natural plant organic matter). | [0044] 11. The solid support or solid support material is chosen to promote proximity to some element of the enhanced weathering process (e.g. finely ground rock, top soil plant organic matter, or anything else that might be deployed with the enhanced weathering technology)| [0045] In some aspects, natural (and/or unnatural) acids (and/or bases) can be created naturally (and/or unnaturally) in situ and react with the charged cation, a divalent metal cation and/or a monoatomic dication. | [0046] Brief Description of the Drawings | [0047] Figure 1A shows optical density readings from a 4-nitrophenyl acetate (4-NPA) assay performed using Carbonic Anhydrase (CA) obtained from bovine blood. The blood was obtained from Amazon steak meat. | [0048] Figure 1 B shows the product titre obtained from a 4-nitrophenyl acetate (4-NPA) assay performed using CA obtained from Amazon steak, Sainsbury’s steak, or pasteurised milk.| [0049] Figure 2A shows a plot of activity slopes of CA obtained commercially, bovine serum, blood obtained from Amazon steak, Sainsbury’s steak, or pasteurised milk. | [0050] Figure 2B shows an activity kinetic plot of the buffer used in Figure 2A only, as negative control.| [0051] Figure 2C shows an activity kinetic plot for CA at various dilutions. | [0052] Figure 2D shows an activity kinetic plot for CA obtained from blood obtained from Amazon steak meat. | [0053] Figure 3 shows a bar graph showing relative activity of commercially-obtained CA and CA obtained from blood obtained from Amazon steak meant at various temperatures.Figure 4 shows the product titre obtained from a 4-nitrophenyl acetate (4-NPA) assay performed using commercially-obtained CA or CA obtained from blood obtained from Amazon steak meat. Each CA was immobilised to different solid supports, namely sand, silica gel, calcium carbonate, or dolomite. | [0054] Figure 5 shows that CA obtained from blood obtained from steak immobilised to silica gel in sea water in acidic conditions is active. | [0055] Figure 6 shows 6x 50 mL falcon tubes containing either 0, 1 , or 10 mL of crude CA from a commercial source added to 0.5 g of raw “R” or processed “P” basalt, supplemented with 0.1 M NaPi pH 7.0 (25 mL). | [0056] Figure 7 shows a bar graph showing that CA obtained from animal blood immobilised on CaCO3 (chalk) can turn over 4-NPA product up to 60°C. | [0057] Figure 8 shows a bar graph showing CA-containing samples produced more CO2 compared to the buffer only controls. | [0058] Figure 9 shows a bar graph showing variation of measured %CO2 equivalents using different basalt carriers. Rb: Remin basalt; Db: Duntilland basalt; SG: silica gel. | [0059] Figure 10 shows a bar graph showing variation of measured %CO2 equivalents when using different basalt carriers and steel slag with tap water or buffer during the CA reaction. | [0060] Figure 11 shows a bar graph showing variation of measured %CO2 equivalents when using different basalt carriers, including basalt from Dentilland, Remin, and Crag Mill, with tap water during the CA reaction. | [0061] Figure 12 shows a bar graph showing the effect of different process conditions on CO2 capture by CA immobilised on Dentilland basalt performed in packed bed reactor, “w.r.t” means “with respect to”. | [0062] Figure 13 shows a bar graph showing the effect of CO2 gas flow on the CO2 capture by CA immobilised on Dentilland basalt performed in packed bed reactor, “w.r.t” means “with respect to”. | [0063] Figure 14 shows a bar graph showing the enzyme activity of supernatant (Sup after...), wash fractions (Wash 1 and Wash 2) and the supernatant after reaction (Sup after the reaction) were determined using 4NPA assay. | [0064] Figure 15A shows a bar graph showing variation of 4NPA activity of samples taken from the plots of the field pre-trial after 1 week and 2 weeks post-application of the CA source to the soil. The numbers on the x-axis denote plot numbers, which are provided in Table 3.Figure 15B shows a bar graph showing variation of CO2 equivalents of samples taken from the plots of the field pre-trials after 1 week and 2 weeks post-application of the CA source to the soil. The numbers on the x-axis denote plot numbers, which are provided in Table 3.| [0065] Figure 15C shows a bar graph showing percentage carbonate formation measured from samples taken from plots of the field pre-trials after 2, 4, and 6 weeks post-application of the CA source to the soil. | [0066] Detailed Description of the Invention | [0067] The disclosure is based on the development of new methods and compositions to sequester carbon in enhanced weathering by application of Carbonic Anhydrase, and optionally rock, to material such as soil or earth. This accelerates the rate of carbon sequestration. | [0068] In one aspect of the invention, Carbonic Anhydrase (and optionally rock) is applied to soil or earth. Advantageously, immobilisation of the Carbonic Anhydrase onto a solid support retains the Carbonic Anhydrase in the top soil. Similarly, engineering of the Carbonic Anhydrase to retain it at a defined soil depth is also advantageous. | [0069] Another aspect of the invention provides a mixture comprising Carbonic Anhydrase and seed, optionally wherein the Carbonic Anhydrase is immobilised to a solid support that may optionally be the seed. Another aspect of the invention provides a mixture comprising Carbonic Anhydrase and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0070] Another aspect of the invention provides a mixture comprising Carbonic Anhydrase and rock, optionally wherein the Carbonic Anhydrase is immobilised to a solid support that may optionally be the rock. | [0071] Another aspect of the invention provides a mixture comprising carbonic anhydrase, rock and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0072] Carbonic anhydrase enzymes are well-known in the art. This enzyme was first identified in 1933, in red blood cells of cows. Since then, it has been found to be abundant in all mammalian tissues, plants, algae and bacteria. This ancient enzyme has three distinct classes (called alpha, beta and gamma carbonic anhydrase). Members of these different classes share very little sequence or structural similarity, yet they all perform the same function and typically require a zinc ion at the active site. | [0073] PDB entries 1ca2 , 1ddz and 1thj are examples of the alpha, beta and gamma Carbonic Anhydrase enzymes, respectively.In some embodiments, the CA is from an animal species, for example cattle or sheep. | [0074] In some embodiments, the CA enzyme may be obtained, isolated or purified from animal blood, typically non-human mammalian blood, for example bovine or ovine blood. | [0075] In some embodiments, the CA enzyme may be produced recombinantly, typically expression of an exogenous gene in a host species. The host species is typically a microbial cell and/or the enzyme gene is expressed under a controllable promoter. For example, a mammalian carbonic anhydrase can be expressed in bacterial (e.g. E.Coli) or yeast (e.g. S.Cerevisiae or S.Pombe) cell, typically on a recombinant expression cassette. | [0076] Some aspects of the invention involve one or more of the following numbered features: | [0077] 1. Enzyme + solid support: identify pairing with retained enzyme activity and greatest imparted stability | [0078] 2. Select solid support to improve longevity of the accelerated enzyme effect on the pre- biologically treated version of enhanced weathering (whatever rock and/or system is being deployed) | [0079] 3. Select solid support to prevent leaching too deep into the soil, which is then too far from the enhanced weathering environment | [0080] 4. Select solid support to prevent deactivation and/or degradation by protease or other active entities in the environment of the enhanced weathering process. | [0081] Enzymes | [0082] The term enzyme is to be given its usual meaning in the art, i.e. a protein that accelerates or catalyses chemical reactions. An enzyme may have one or more active sites that bind to a substrate or selection of substrates. An enzyme may be naturally occurring or it may be of synthetic origin. | [0083] An enzyme is capable of catalysing a given reaction, and is sometimes thereof rereferred to as “an activity” or an “enzyme activity”. For example, a protein capable of catalysing the conversion of carbon dioxide and water into bicarbonate and protons is a Carbonic Anhydrase activity. | [0084] Suitable enzymes can include, for example: enzymes comprising natural and unnatural amino acids, chemical modifications or post-translational modifications; natural enzymes; wild-type enzymes; recombinant enzymes; enzymes produced by directed evolution, de novo design or the genetic fusion of peptide or protein domains; peptide catalysts; nucleic acid enzymes (e.g.ribozymes or DNA enzymes); hybrid catalysts; monomeric, dimeric or multimeric enzymes; enzymes produced in vivo or in vitro for example by solid-phase synthesis. | [0085] In an active enzyme system, the enzymes are provided under conditions suitable for enzyme activity, for example in the necessary physical and chemical conditions for enzyme activity. For the reaction to proceed, reagents will be needed, along with any necessary cofactor such as Zinc. Metal ions may also be included in the active enzyme system. | [0086] In the present invention, the enzyme is typically carbonic anhydrase. | [0087] In some embodiments, the Carbonic Anhydrase comprises an animal carbonic anhydrase. Optionally, the animal Carbonic Anhydrase comprises a mammalian carbonic anhydrase, optionally bovine erythrocyte Carbonic Anhydrase and/or human carbonic anhydrase. | [0088] In some embodiments, the Carbonic Anhydrase comprises a plant carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a bacterial carbonic anhydrase.| [0089] In some embodiments, the Carbonic Anhydrase comprises an alpha carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a beta carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a gamma carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a delta carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a zeta carbonic anhydrase. | [0090] In some embodiments, the Carbonic Anhydrase used in the method of the present invention comprises one or more classes of carbonic anhydrase. | [0091] Enzyme activity and stability | [0092] An enzyme in an active state, i.e. an active enzyme, is capable of catalysing a chemical reaction. | [0093] In one embodiment, an enzyme is stable if it remains in an active state for a period of time. In some embodiments, the period of time is at least a day, at least three days, at least 1 week, at least 2 weeks, at least 1 month, at least 6 weeks, at least 2 months, at least 3 months, at least 6 months, at least 9 months, at least 12 months, at least 18 months or at least 2 years, optionally wherein the period of time is at least one month or at least one year. | [0094] In some embodiments, the enzyme is active when present in soil as described herein, typically exposed to the elements and weather. | [0095] In some embodiments, the activity of an enzyme can be measured by the yield of the product produced by the enzymatic reaction, or by measuring conversion, depletion or consumption of the substrate. In some embodiments, the enzyme is active if the yield of product is about 40% or more, about 50% or more, about 60% or more, about 70% or more, about 80% or more,about 90% or more, or about 100% of the yield from the initial use cycle, when assessed under the same reaction conditions. | [0096] In some embodiments, the enzyme is stable over a given time period if, over that time period, the yield of product is about 40% or more, about 50% or more, about 60% or more, about 70% or more, about 80% or more, about 90% or more, or about 100% of the activity within one hour of immobilisation, when assessed under the same reaction conditions. | [0097] In some embodiments, the enzyme is active after 4 weeks or three months. In some embodiments, the enzyme is active over that time period if the yield of product is about 40% or more, about 50% or more, about 60% or more, about 70% or more, about 80% or more, about 90% or more, or about 100% of the activity within one hour of immobilisation, when assessed under the same reaction conditions. | [0098] In one aspect of the invention, a homologue of a reference enzyme has higher stability than the reference enzyme under the specified reaction process conditions. For example, a reference enzyme from a first species may catalyse a stated reaction when immobilised, but a homologue of that enzyme catalyses the same stated reaction with higher activity when immobilised to the same solid support. Typically, the homologue enzyme will have higher activity after a period of time, for example after weeks or months, and the long-term stable activity can be more valuable in terms of the efficiency of large scale biocatalysis than the initial activity shortly after immobilisation. Therefore, identifying homologues that are active and stable for a period of weeks, months or longer, is particularly advantageous. | [0099] Identification of one or more homologues | [0100] In one embodiment, an enzyme for immobilisation is identified by identifying two or more enzymes with different polypeptide sequences that catalyse a chemical reaction of interest. In some embodiments, the two or more enzymes comprises the enzyme of interest and one or more enzymes that are homologues of that enzyme of interest. In some embodiments, identifying the two or more enzymes is performed in a search, typically a search of one or more bioinformatic databases using one or mor bioinformatic search tools. | [0101] Bioinformatic databases and tools are well-known in the art. For example, a summary of useful bioinformatics tools can be found at www.ebi.ac.uk/tools and with sequence similarity searching tools collected at https://www.ebi.ac.uk/Tools/sss/ | [0102] In some embodiments, identifying the two or more enzymes is performed in a search wherein an amino acid sequence is an input. In some embodiments, identifying two or more enzymes is performed in a search wherein a nucleic acid sequence is an input. The input sequence is typically a reference enzyme sequence from a first species. In some embodiments, the search output is one or more amino acid sequences. In some embodiments, the search output is oneor more nucleic acid sequences. Typically, the search output includes an enzyme sequence from a different species from the reference sequence, that has a different sequence from the sequence of the reference enzyme, and that catalyses the same chemical reaction. | [0103] In some embodiments, the search comprises use of one or more sequence similarity searching methods. Optionally, the sequence similarity searching method is one or more of: BLAST (Basic Local Alignment Search Tool), optionally NCBI BLAST, PSI-BLAST, or PHI-BLAST; FASTA, optionally FASTA, SSEARCH, PSI-SEARCH, PSI-SEARCH2, GGSEARCH, GLSEARCH, or FASTM/S/F. | [0104] In some embodiments, the search comprises a classical literature search to identify additional mutations of the enzyme of interest. | [0105] In some embodiments, identifying the two or more enzymes comprises search which comprises one or more, optionally all, of use of one or more sequence similarity searching methods, alignment of multiple sequences, identifying an enzyme of interest and identifying sequences that are close to the enzyme of interest using a database of protein families, and identify additional mutations of the enzyme of interest. Optionally, two or more sequences are aligned again to remove redundancies. | [0106] Selection of one or more homologues | [0107] The present invention may involve the identification and selection of an enzyme and a solid support to which the enzyme can be immobilised. | [0108] In one aspect of the invention, the enzyme is identified by a method that comprises a step comprising identifying two or more enzymes with different polypeptide sequences that catalyse a chemical reaction of interest. In some embodiments, the two or more enzymes comprises one enzyme which is the enzyme of interest and one or more enzymes which are homologues of the enzyme of interest. | [0109] In some embodiments, properties of the one or more homologues are compared to properties of the enzyme of interest to select for one or more homologues for immobilisation. | [0110] Enzymatic activity is known to be influenced by factors including, but not limited to, temperature. Typically, the optimal temperature for an enzyme is the temperature which allows the enzyme to function at maximal activity. | [0111] In some embodiments, the enzyme is derived from a mesophilic organism. In some embodiments, the enzyme is derived from a cryophilic organism. | [0112] In some embodiments, the enzyme or homologue is mesophilic. In some embodiments, the enzyme or homologue is cryophilic.In some embodiments, the optimum temperature of the enzyme or homologue is 70°C or less, for example between 40°C and 70°C . In some embodiments, the optimum temperature of the enzyme or homologue is 50°C or less, for example between 40°C and 50°C. In some embodiments, the optimum temperature of the enzyme or homologue is 40°C or less, for example between 30°C and 40°C. In some embodiments, the optimum temperature of the enzyme or homologue is 30°C or less, for example between 20°C and 30°C. In some embodiments, the optimum temperature of the enzyme or homologue is 20°C or less, for example between 10°C and 20°C. In some embodiments, the optimum temperature of the enzyme or homologue is 15°C or less, for example between 5°C and 15°C. In some embodiments, the optimum temperature of the enzyme or homologue is 5°C or less, for example between minus 20°C and plus 5°C or between minus 20°C and 0°C. | [0113] In a further embodiment, such enzymes or homologues are engineered to improve their stability. | [0114] Selection of enzyme or homologue according to temperature of geographical region| [0115] Enzymatic activity is known to be influenced by factors including, but not limited to, temperature. Typically, the optimal temperature for an enzyme is the temperature which allows the enzyme to function at maximal activity. | [0116] The present invention may involve the identification and selection of an enzyme according to the temperature of the geographical location or region to which the enzyme is to be applied. The selection of the enzyme may be determined according to one or more of previous temperature recordings, current temperature recordings, and predictions of future temperature. In some embodiments, the temperature comprises or consists of the temperature of air. In some embodiments, the temperature comprises or consists of the temperature of top soil. In some embodiments, the temperature comprises or consists of the average temperature of the geographical location or region. In some embodiments, the average temperature comprises or consists of a yearly average. In some embodiments, the average temperature comprises or consists of the average temperature over the course of a growing season of a crop. In some embodiments, the average temperature comprises or consists of the day average temperature. In some embodiments, the average temperature comprises or consists of the night average temperature. In some embodiments, the average temperature comprises or consists of the day average temperature and the night average temperature. | [0117] Typically, methods of sequestering carbon according to the present invention may occur in geographical locations or regions where the average temperature is about 70°C or less. Accordingly, an enzyme or homologue that has an optimal activity at a temperature of about 70°C or less may be selected. In some embodiments, the optimal activity of the enzyme orhomologue occurs at 70°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at60°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 50°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at40°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 30°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at20°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 15°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 10°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 5°C or less. | [0118] Different homologues may be selected for use in a method of sequestering carbon according to the present invention, depending on the geographical location. For example, a homologue with a lower optimal temperature may be preferentially selected for use in a colder geographical location than a warmer geographical location. | [0119] Accordingly, in some embodiments, the optimal temperature for the enzymatic activity of an enzyme or homologue corresponds to the average temperature of the geographical location or region to which the enzyme is applied or will be applied. In some embodiments, the optimal temperature is within 20°C of the average temperature of the geographical location or region. For example, if the average temperature of the geographical location or region is 20°C, the optimal temperature for enzyme activity would fall between 0°C and 40°C. In some embodiments, the optimal temperature is within 15°C of the average temperature of the geographical location or region. In some embodiments, the optimal temperature is within 10°C of the average temperature of the geographical location or region. In some embodiments, the optimal temperature is within 5°C of the average temperature of the geographical location or region. | [0120] Cells comprising carbonic anhydrase | [0121] The disclosure typically contemplates the use of an isolated, purified or partly-purified carbonic anhydrase enzyme, for example that has been extracted from its natural environment by an isolation or purification process. This may be purification such that the carbonic anhydrase is the majority component, or substantially the only component, of a preparation following a purification step (e.g. the enzyme has been purified using one or more chromatography steps as are well-known in the art). The enzyme may alternatively have been only slightly isolated from the cell in which it was expressed, for example the enzyme can be provided in a lysate.In some embodiments the enzyme is not separated from the cell in which it is expressed. The carbonic anhydrase is applied to the soil while still inside a cell, i.e. a cell comprising the enzyme is applied to the soil. The cell may be alive or dead. The cell should contain carbonic anhydrase protein, and/or have the function of being able to express carbonic anhydrase under appropriate conditions. This ability requires the presence of a nucleic acid sequence that encodes a carbonic anhydrase enzyme. The carbonic anhydrase may be endogenous to the cell, or may be exogenous (e.g. expressed recombinantly). | [0122] Typically, the cell is a microorganism. In this aspect of the invention, a method of sequestering atmospheric carbon comprises the step of applying a microbe and optionally rock to soil, wherein the microbe expresses (or has previously expressed, or is able to express) carbonic anhydrase. Typically, the microbe endogenously expresses carbonic anhydrase. | [0123] The microbe typically comprises one or more single-celled organisms, optionally a prokaryotic cell, a fungal cell, a microalgae cell, an archaea cell, and/or a bacterial cell. | [0124] In some embodiments, the microbe: is obtained from or is present in milk, fermented milk, yogurt or kefir; comprises or consists of lactobacillus, lactococcus, leuconostoc, streptococcus or enterococcus bacteria; comprises or consists of Saccharmocyes Cerevisiae, baker’s yeast, brewer’s yeast or Schizosaccharomyces pombe', comprises or consists of compost starter containing organisms; comprises or consists of a combination of at least one bacterium and at least one fungus, optionally wherein the at least one bacterium comprises an Actinomycetes. | [0125] Table 3 in the Examples below demonstrates the use of carbonic-anhydrase expressing cells from a wide range of sources, including chicken serum, potatoes, bakers’ yeast, brewers’ yeast, compost starter, yogurt (comprising Lacticaseibacillus casei Shirota), eggs, raw goats milk, beef, pork, raw cows milk and grass. Each of these sources of CA is provided as a separate embodiment of the invention. These cells themselves can be used according to the present disclosure, or the enzyme can be extracted, isolated or purified and used as a purified enzyme preparation or a part-purified extract.In some embodiments, the cell comprising carbonic anhydrase may be immobilised to rock, typically particulate rock. Any technique of immobilising the cell to the rock can be used, for example adsorption. | [0126] Immobilised enzymes | [0127] Compared to free enzymes in solution, immobilised enzymes are typically more robust and more resistant to environmental changes. | [0128] Multiple copies of a single enzyme may be attached to a single support, for example a single bead or other solid support as described herein e.g. waste material such as a corn husk or fragment thereof, the rock component itself, a seed, or a plant. These may be attached in an identical fashion, or different copies of a single functional molecule may be attached differently. This can provide, for example, improved activity for a single type of functional molecule when the structure is placed under different bulk environmental conditions. | [0129] In some embodiments, two or more different Carbonic Anhydrase enzymes (i.e. different sequences) are attached to each support, e.g. each bead, each rock particle, each seed, or each plant. These may each be present once, or may each be present multiple times. | [0130] Solid Supports | [0131] The invention typically involves immobilising an enzyme, typically Carbonic Anhydrase, to a solid support. The solid support may comprise controlled pore glass, polystyrene, sepharose or alginate. In some embodiments, the solid support is particulate. The solid support may comprise beads, for example, controlled pore glass beads, polystyrene beads or buoyant beads. In some embodiments, the solid support is a resin. In some embodiments, the solid support is magnetic, for example magnetic beads. In one embodiment, the solid support comprises Poly(styrene-divinylbenzene). | [0132] Typically, the solid support is available at a low cost to ensure commercial viability of the method. | [0133] In some embodiments, the enzyme is directly immobilised onto the rock, e.g. finely ground rock, used for the enhanced weathering process. | [0134] Plants and seeds as solid supports | [0135] Without wishing to be bound by theory, the inventors have found that inoculating an enzyme such as Carbonic Anhydrase onto a plant seed or plant root has many advantages over microbial inoculations, including one or more of: | [0136] - the enzyme is easier to scale than the microbial inoculant in an expression vessel.- the enzyme dosing onto the seed or plant can be controlled much more easily than inoculated microbial systems in the soil | [0137] - the enzyme might be more efficient than other related microbial approaches at helping to sequester carbon for agricultural fields | [0138] - the enzyme can be modified for improved properties and still considered non-GMO compared to the microbial inoculant. | [0139] The inventors also consider, without being bound by theory, that the enzyme might be more active deeper in the soil near the plant roots where biomass decomposition leads to enhanced CO2 levels. | [0140] Notably, rock such as basalt is not required for Carbonic Anhydrase enzyme to be inoculated on seeds or plant. The salinity + CO2 + water in the soil is suitable to carry out the carbon sequestration. Rock may be added in some embodiments. | [0141] In certain embodiments, the plant or seed is sprayed with a liquid comprising the enzyme, wherein the enzyme is typically carbonic anhydrase. Methods of spraying plants and plant seeds are known in the art. | [0142] Seed as a solid support | [0143] In one aspect the solid support is a seed. In some embodiments, the enzyme is immobilised onto a seed. Typically, the seed is a variety used in agriculture. In some embodiments, the enzyme is directly immobilised onto the seed. In some embodiments, the enzyme is directly immobilised onto the seed coat. | [0144] Certain non-limiting aspects and embodiments relate to coating, dipping or spraying agricultural seeds with a liquid containing Carbonic Anhydrase enzyme, which then achieves immobilization of the enzyme onto the hard shell of the seed before it is placed in the soil. The Carbonic Anhydrase enzyme then remains in/around the plant root system for a prolonged period of time, for example one month or more. | [0145] Typically, the enzyme is immobilised onto the seed before the seed is sown. Accordingly, in some embodiments, the seed is contacted with a mixture comprising the enzyme, typically a liquid mixture. In some embodiments, the seed is sprayed with the mixture. In some embodiments, the seed is stirred with or into the mixture. In some embodiments, the seed is introduced to the mixture and the mixture is aerated. In some embodiments, the seed is submerged in the mixture. In some embodiments, the seed is placed on an article comprising the mixture. In some embodiments, the seed is placed within an article comprising the mixture. In some embodiments, the seed is placed underneath an article comprising the mixture. In some embodiments, the seed is placed on an article soaked in the mixture. In someembodiments, the seed is placed within an article soaked in the mixture. In some embodiments, the seed is placed underneath an article soaked in the mixture. Following contact with a liquid comprising the enzyme, the seed is typically removed from contact with the enzyme liquid, and may optionally be allowed to dry in ambient surroundings or be subjected to an active drying step. | [0146] Some agricultural crop seeds undergo seed priming prior to sowing. Seed priming is a process of regulating the germination process by managing the temperature and seed moisture content. In some embodiments, the seed is contacted with the enzyme (e.g. mixture comprising the enzyme) prior to priming. In some embodiments, the seed is contacted with the mixture during priming. In some embodiments, the seed is contacted with the mixture after priming. | [0147] Accordingly, the present disclosure provides a mixture comprising Carbonic Anhydrase and seed, wherein the Carbonic Anhydrase is immobilised to the seed. In some embodiments, the mixture is sown into agricultural land. | [0148] Immobilising the enzyme to a seed coat may be particularly useful commercially, as this may allow for reduced labour time on agricultural land and/or reduce the need for additional steps to supply the enzyme to the top soil separately to the seed. | [0149] Plant as a solid support | [0150] In another aspect, the solid support is a plant. Typically, the plant is suitable for growing as an agricultural crop. In some embodiments, the enzyme is directly immobilised onto the plant. The enzyme may be immobilised onto one or more parts of the plant, including but not limited to, the plant root, the plant stem, the plant leaf, the plant bulb, and the plant tuber. In some embodiments, the enzyme is directly immobilised onto the plant stem. In some embodiments, the enzyme is directly immobilised onto the plant bulb. In a further embodiment, the enzyme is directly immobilised onto the bulb tunic. In some embodiments, the enzyme is directly immobilised onto the plant tuber. In some embodiments, the enzyme is directly immobilised onto the plant tuberous root. In a further embodiment, the enzyme is directly immobilised onto the tuber periderm. In a preferable embodiment, the enzyme is directly immobilised onto the plant root. In some embodiments, the plant is a seedling. In some embodiments, the plant is a mature plant. | [0151] The enzyme may be immobilised onto the plant before it is planted in agricultural land. Accordingly, in some embodiments, the plant is contacted with a mixture comprising the enzyme. In some embodiments, the plant is sprayed with the mixture. In some embodiments, the plant is dipped into the mixture. In some embodiments, the plant is submerged in the mixture. In some embodiments, the plant is watered with the mixture. For example, the enzymemay be immobilised onto the plant root by contacting the plant root with a mixture comprising the enzyme, optionally wherein the contacting occurs by one or more of spraying, dipping, submerging, and watering. | [0152] The enzyme may be immobilised onto the plant after it is planted in agricultural land. Accordingly, in some embodiments, the plant is contacted with a mixture comprising the enzyme. In some embodiments, the plant is sprayed with the mixture. In some embodiments, the plant is watered with the mixture. In some embodiments, the mixture is provided to the plant through an irrigation system. For example, the enzyme may be immobilised onto the plant root by contacting the plant root with a mixture comprising the enzyme, optionally wherein the contacting occurs by watering the plant with the mixture, optionally wherein the watering is performed using an irrigation system. | [0153] Species of plants and seeds | [0154] In some embodiments, the plant or seed is a crop plant or crop plant seed, optionally a crop plant of agronomic importance which is cultivated for food, animal feed, fiber, fuel, and/or industrial purposes. In one embodiment, the crop plant is a commercial crop plant. A commercial crop plant is a plant cultivated to produce a harvested horticultural product that is for sale and/or profit, as well as subsistence crops which may be grown to support other agricultural products, such as livestock. | [0155] In one embodiment, the plant is a commercial crop plant. In one embodiment, the commercial crop plant is a compatible crop selected from the group consisting of species of the genus Triticum, Brassica, Gossypium, Zea, Corchorus, Saccharum, Medicago, Lolium, Coffea, Camellia, Oryza, Hordeum, Boehmeria, Nicotiana and Cannabis. | [0156] In one embodiment, the commercial crop is selected from the group consisting of the species Triticum aestivum, Brassica napus, Brassica rapa, Brassica juncea, Gossypium hirsutum, Gossypium barbadense, Gossypium arboretum, Gossypium Herbaceum, Zea mays, Medicago sativa, Lolium multiflorum, Corchorus capsularis, Saccharum officinarum, Cannabis sativa, Coffea Arabica, Coffea Robusta, Camellia sinensis, Oryza sativa, Hordeum vulgare, Boehmeria nivea and Nicotiana tabacum. | [0157] In one embodiment, the crop plant is a cereal plant. Cereal plants include, for example, wheat [Triticum), rice [Oryza), barley [Hordeum), corn [Zea). | [0158] In one embodiment, the cereal plant is selected from wheat, and barley. | [0159] In one embodiment, the cereal plant is a wheat plant. | [0160] The inventors have found that growing a plant or seed that has been contacted with an enzyme such as Carbonic Anhydrase results in an increase in soil carbon and/or an increase in yieldof the plant being cultivated in the soil. The plants may be crop plants, which are known in the art and include for example wheat, canola, and barley. Applying the enzyme to the plant or seed can result in increased yield of plant relative to untreated plants. The inventors have further found that the soil in which these plants are grown can have increased organic carbon content relative to soil in which untreated plants are grown. | [0161] In some embodiments, the present disclosure to enhancement of agricultural soils, mitigating atmospheric carbon dioxide, and providing agronomic benefits to crop plants. Additionally, the present disclosure relates in part to methods and compositions for increasing soil organic carbon in soil, and increasing crop plant yield. | [0162] In some embodiments, the soil is contacted with the enzyme. The soil may be contacted with the enzyme prior to planting a plant, for example before, during, or after tilling the soil in preparation for planting. In other embodiments, the soil may be contacted with the enzyme after the plant has been planted. In some embodiments, the soil is contacted with the enzyme by planting in the soil plants that have been contacted with the enzyme. | [0163] In some embodiments, the step of contacting with the enzyme comprises applying the enzyme to seeds of the plant prior to planting. | [0164] In some embodiments, the step of contacting with the enzyme comprises applying the enzyme to seedlings of the plant. | [0165] In some embodiments, the step of contacting with the enzyme comprises applying the enzyme to a plot of soil that is cultivated, such that the enzyme is retained by the soil as the crops are rotated, even in the absence of crops for periods of time. | [0166] In one embodiment, the plants are contacted with the enzyme as a seed coating before, during or after one or more of the stages of germination of a seed, or as a root inoculant of a seedling. For example, the enzyme may be applied as a seed coating to seeds at large scale prior to sowing a crop. | [0167] In some embodiments, the enzyme is provided as a composition comprising an agriculturally acceptable excipient. | [0168] As used herein, an "agriculturally acceptable excipient" refers to an essentially inert substance that can be used as a diluent and/or carrier for the enzyme and is not detrimental to the plant or seed. | [0169] In one embodiment, the agriculturally acceptable excipient is a solid or liquid carrier. Suitable solid carriers include mineral earths (e.g., calcium phosphate, calk, clay, diatomaceous earth, dolomite, kaolin, silicates, silica gels, talc, etc), cellulose, and starch. Suitable liquid carriers include water, or any other liquid solvents which are not toxic to the seed or the plant.In one embodiment, the composition comprises an agriculturally acceptable additive. As used herein, an "agriculturally acceptable additive" is an additive that may assist in or enhance the performance of the enzyme and/or the plant or seed, and is not detrimental to the one or more enzyme or to the plant or seed. Examples of agriculturally acceptable additives include preservatives, stabilizers, nutrition enhancers, wetter-spreaders, stickers (adhesives), penetrants, root promoters, fungicides, urea, fertilisers, pesticides, fulvic acid, humus, nanoparticles/nanomaterials. | [0170] In some embodiments, the enzyme may be provided as a composition in the form of a dried powder, a spray, a slurry, a sachet, a liquid, a jelly, a seed coating, an enhancer, and/or combinations thereof. In some embodiments, the composition is in the form of a seed coating, a foliar spray, granule, powder, soil drench or a root dip. | [0171] In some embodiments, the composition is in the form of a seed coating. | [0172] In some embodiments, the composition is in the form of a foliar spray. | [0173] In some embodiments, the composition is in the form of a soil drench. | [0174] In some embodiments, the composition is in the form of a root dip. | [0175] Solid support cost | [0176] The invention typically utilises solid supports that are available at a low cost to ensure commercial viability of the method when applied at a large scale, for example to be spread over acres or hectares of ground. | [0177] In some embodiments, the solid support has a procurement cost of $20 or less per kg. Typically, the solid support has a procurement cost of $10 or less per kg. It is beneficial if the solid support has a procurement cost of $5 or less per kg and beneficial further still if the solid support has a procurement cost of $1 or less per kg, or $0.5 or less per kg. | [0178] Source of alternative solid supports | [0179] In some embodiments, the solid support comprises plant matter. In some embodiments, the plant matter comprises vegetable matter, optionally fibrous matter. In some embodiments the vegetable matter comprises waste matter from the farming process and/or food chain. In some embodiments, the waste matter comprises corn husks. | [0180] In some embodiments, the solid support comprises animal matter, optionally fibrous matter.| [0181] Typically, the solid support is obtained from waste matter. In some embodiments, the waste matter comprises or consists of produce such as fruit and/or vegetables (e.g. corn or corn husks) that are too old, spoiled or rotten to be sold, or are inedible. In some embodiments, the waste matter comprises fibrous plant or animal matter that is too old, spoiled or rotten to besold, or is inedible. In certain embodiments, the solid support is from material that would otherwise be seen as low or no value, or as a waste product. In some embodiments, the solid support is from commercial waste or household waste. | [0182] Typically, the material is robust enough not to degrade significantly, or at all, over a period of at least 6 months, or least one year. | [0183] Bead solid supports | [0184] In some embodiments, the solid support is a bead. Solid supports that are beads are well- known in the art. In some embodiments, the solid support is a resin bead. Resin beads are well-known in the art. Resin beads are typically essentially spherical. | [0185] In some embodiments, the bead is porous. In porous beads, binding sites can also be internal, leading to higher loading of enzyme. | [0186] The beads may be from 10 micron to 1500 micron diameter, typically 100 micron to 1200 micron, for example 150 micron to 300 micron diameter. | [0187] In some embodiments, the beads are methacrylate beads, for example epoxy methacrylate beads, epoxy/butyl methacrylate beads, amino C2 methacrylate beads or Amino C6 methacrylate beads. | [0188] The inventors have successfully immobilised enzymes using a variety of beads including amine-functionalised beads and epoxy-functionalised beads. | [0189] Epoxy resins | [0190] Beads that are functionalised with epoxides are known as “epoxy” functionalised resins, or epoxy-resins. The IIIPAC name for an epoxide group is an oxirane. Epoxides react with nucleophiles and in the context of protein immobilisation, the reactive residues will typically be Lys and Cys (and sometimes His). Surface epoxy groups on beads therefore allow direct covalent binding of proteins or peptides, which can be achieved by simple incubation of the protein or peptide with the epoxy-bead, for example overnight. | [0191] Epoxy-functionalised beads can be used in the invention because they form very stable covalent linkages. | [0192] In some embodiments, the bead is an epoxy-methacrylate bead. In some embodiments, the bead is an epoxy/butyl methacrylate bead. | [0193] In some embodiments, the pore diameter of the epoxy beads is 300 to 1800 A. Optionally, the pore diameter is 300 to 600 A, 450 to 600 A, or 1200 to 1800 A. In some embodiments, the total moisture of the beads is 50 to 80%. | [0194] Optionally, the total moisture of the beads is 50 to 65%, or 70 to 80%.In some embodiments, a minimum of 85% of the beads are perfectly spherical. Optionally a minimum of 95% of the beads are perfectly spherical. | [0195] In one embodiment, the epoxy beads are epoxy/butyl methacrylate beads, wherein the particle size range is 250 to 1000 micron, the pore diameter is 450 to 650 A, and the total moisture is 70 to 80%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage at 2 to 8°C. Optionally, a minimum of 85% of the beads are perfectly spherical. | [0196] In one embodiment, the epoxy beads are epoxy methacrylate beads, wherein the particle size range is 150 to 300 micron, the pore diameter is 300 to 600 A, and the total moisture is 50- 65%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage from 2 to 8°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0197] In one embodiment, the epoxy beads are epoxy methacrylate, wherein the particle size range is 150 to 300 micron, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage at 2 to 8°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0198] Amine-functionalised resins | [0199] Beads that are functionalised with amines are known as amine-functionalised beads or amine- functionalised resins. Amine functional groups form covalent amide bonds with proteins or polypeptides. Amine-functionalised beads are generally pre-activated with glutaraldehyde, prior to ionic polypeptide immobilisation. pH adjustment during incubation results in the formation of an amide bond between the bead and the protein or polypeptide. | [0200] In some embodiments, the bead is an amino C2 methacrylate bead. In some embodiments, the bead is an amino C6 methacrylate bead. | [0201] In some embodiments, the particle size range of the amine-functionalised beads is 150 to 300 micron. | [0202] In some embodiments, the pore diameter is 600 to 1800 A. Optionally, the pore diameter is 600 to 1200 A, or 1200 to 1800 A. | [0203] In some embodiments, the total moisture of the beads is 62 to 80%. Optionally, the total moisture is 62 to 72%, or 70 to 80%. | [0204] In some embodiments, a minimum of 95% of the beads are perfectly spherical. | [0205] In one embodiment, the amine-functionalised beads are amino C2 methacrylate beads, wherein the particle size range is 150 to 300 micron, the pore diameter is 600 to 1200 A, andthe total moisture is 62 to 72%. The functional group is amino (short spacer). The beads are typically stable at pH 3 to pH 10, and suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0206] In one embodiment, the amine-functionalised beads are amino C2 methacrylate beads, wherein the particle size range is 150 to 300 micron, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is amino (short spacer). The beads are typically stable at pH 3 to pH 10, and are suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0207] In one embodiment, the amine-functionalised beads are amino C6 methacrylate beads, wherein the particle size range is 150 to 300 micron, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is amino (short spacer). The spherical beads are stable at pH 3 to pH 10, and are suitable for storage at 2 to 20 oC. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0208] Adsorbent resins | [0209] In some embodiments, the bead is an adsorbent resin bead. Adsorbent beads immobilise the protein or peptide by adsorption. Proteins or polypeptides with hydrophobic properties can be efficiently immobilised onto adsorbent beads. Adsorbent resins are water-insoluble carriers that allow physical adsorption of an enzyme onto its surface. | [0210] In some embodiments, the bead is a polystyrenic, non-functionalised resin bead. In some embodiments, the bead is an octadecyl methacrylate bead. In some embodiments, the bead is a polymethacrylic/divinylbenzene bead. In some embodiments, the bead is a polymethacrylic/divinylbenzene macroporous bead. In some embodiments, the polymer structure is polymethacrylic crosslinked with divinylbenzene. | [0211] Adsorbent beads can be used with the invention because they immobilise proteins or polypeptides with high mechanical stability. | [0212] In some embodiments, the particle size range is 300 to 1200 micron. Optionally, the particle size range is 300 to 710 micron, or 350 to 1200 micron. | [0213] In some embodiments, the pore diameter is 220 to 1200 A. Optionally, the pore diameter is 900 to 1100 A, 400 to 650 A, 220 to 340 A, or 350 to 1200 A. | [0214] In some embodiments, the total moisture is 57 to 78%. Optionally, the total moisture is 67 to 78%, 58 to 63%, 57 to 68%, or 60-66%. | [0215] In some embodiments, the typical pore diameter by nitrogen adsorption is 300 A. In some embodiments, the typical pore volume by nitrogen adsorption is 1.2 mL/g. In some embodiments, the typical surface area by nitrogen adsorption is 490 m2/g.In some embodiments, the specific gravity is 1.1. | [0216] In some embodiments, a minimum of 95% of the beads are perfectly spherical. | [0217] In some embodiments, the adsorbent bead has a functional group. Optionally the adsorbent bead has an amino functional group. Optionally, the functional group is non-ionic. | [0218] In one embodiment, the adsorbent bead is a polystyrenic, non-functionalised resin bead, wherein the particle size range is 300 to 710 micron, the pore diameter is 900 to 1100 A, and the total moisture is 67 to 78%. The spherical beads are stable at pH 1 to pH 14, and are suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0219] In one embodiment, the adsorbent bead is an octadecyl methacrylate bead, wherein the particle size range is 300 to 710 micron, the pore diameter is 400 to 650 A, and the total moisture is 58 to 63%. The functional group is amino (short spacer). The spherical beads are stable at pH 2 to pH 10, and are suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0220] In one embodiment, the adsorbent bead is a polymethacrylic/divinylbenzene, nonfunctionalised resin bead, wherein the particle size range is 300 to 710 micron, the pore diameter is 220 to 340 A, and the total moisture is 57 to 68%. The beads are typically stable at pH 1 to pH 14, and are suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0221] In one embodiment, the adsorbent bead is a polymethacrylic/divinylbenzene macroporous, adsorbent resin bead in a non-ionic form, wherein the particle size range is 350 to 1200 micron, the typical pore diameter by nitrogen adsorption is 300 A, the typical pore volume by nitrogen adsorption is 1.2 mL/g, the typical surface area by nitrogen adsorption is 490 m2/g, the specific gravity is 1.1 , and the moisture retention is 60-66%. The functional group is non-ionic and the polymer structure is polymethacrylic crosslinked with divinylbenzene. The spherical beads are stable at pH 0 to pH 14, and the temperature limit is 100°C. | [0222] Ion exchange resins | [0223] In some embodiments, the bead is an ion-exchange resin. In some embodiments, the ionexchange resin is a cation exchange resin or an anion exchange resin. | [0224] In some embodiments, the ion-exchange resin comprises polystyrene crosslinked with divinylbenzene.Examples of epoxy, amine and adsorbent beads that are commercially available from Purolite Ltd. (Llantrisant, Wales, UK) are provided below along with their catalogue numbers. | [0225] Epoxy resins: | [0226] ECR8204F | [0227] • Epoxy-functionalised resin | [0228] • Purolite “perfect bead”: min. 95%. | [0229] • Epoxy methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 300 to 600 A, and the total moisture is 50-65%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage from 2 to 8°C. | [0230] ECR8285 | [0231] • Epoxy-functionalised resin | [0232] • Purolite “perfect bead”: min. 85%. | [0233] • Epoxy/butyl methacrylate beads, wherein the particle size range is 250 to 1000 pm, the pore diameter is 450 to 650 A, and the total moisture is 70 to 80%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage at 2 to 8°C. | [0234] ECR8215F | [0235] • Epoxy-functionalised resin | [0236] • Purolite “perfect bead”: min. 95%. | [0237] • Epoxy methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage at 2 to 8°C. | [0238] Adsorbent resins: | [0239] ECR1090M | [0240] • Adsorbent resin• Purolite “perfect bead”: min. 95%. | [0241] • Functional group: none. | [0242] • Polystyrenic, non-functionalised resin beads, wherein the particle size range is 300 to 710 pm, the pore diameter is 900 to 1100 A, and the total moisture is 67 to 78%. The spherical beads are stable at pH 1 to pH 14, and are suitable for storage at 2 to 20°C. | [0243] ECR8806M | [0244] • Adsorbent resin | [0245] • Purolite “perfect bead”: min. 95%. | [0246] • Octadecyl methacrylate beads, wherein the particle size range is 300 to 710 pm, the pore diameter is 400 to 650 A, and the total moisture is 58 to 63%. The functional group is amino (short spacer). The spherical beads are stable at pH 2 to pH 10, and are suitable for storage at 2 to 20°C. | [0247] ECR1030M | [0248] • Adsorbent resin | [0249] • Purolite “perfect bead”: min. 95%. | [0250] • Functional group: none. | [0251] • Polymethacrylic/divinylbenzene, non-functionalised resin beads, wherein the particle size range is 300 to 710 pm, the pore diameter is 220 to 340 A, and the total moisture is 57 to 68%. The spherical beads are stable at pH 1 to pH 14, and are suitable for storage at 2 to 20°C. | [0252] PAD610 | [0253] • Adsorbent resin | [0254] • Polymethacrylic/divinylbenzene macroporous, adsorbent resin beads in a non-ionic form, wherein the particle size range is 350 to 1200 pm, the typical pore diameter by nitrogen adsorption is 300 A, the typical pore volume by nitrogen adsorption is 1.2 mL/g, the typical surface area by nitrogen adsorption is 490 m2/g, the specific gravity is 1.1 , and the moisture retention is 60-66%. The functional group is non-ionic and thepolymer structure is polymethacrylic crosslinked with divinylbenzene. The spherical beads are stable at pH 0 to pH 14, and the temperature limit is 100°C. | [0255] Amine resins: | [0256] ECR8309F | [0257] • Amine-functionalised resin | [0258] • Purolite “perfect bead”: min. 95%. | [0259] • Amino C2 methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 600 to 1200 A, and the total moisture is 62 to 72%. The functional group is amino (short spacer). The spherical beads are stable at pH 3 to pH 10, and suitable for storage at 2 to 20°C. | [0260] ECR8315F | [0261] • Amine-functionalised resin | [0262] • Purolite “perfect bead”: min. 95%. | [0263] • Amino C2 methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is amino (short spacer). The spherical beads are stable at pH 3 to pH 10, and are suitable for storage at 2 to 20°C. | [0264] ECR8415F | [0265] • Amine-functionalised resin | [0266] • Purolite “perfect bead”: min. 95%. | [0267] • Amino C6 methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is amino (short spacer). The spherical beads are stable at pH 3 to pH 10, and are suitable for storage at 2 to 20°C.Rocks | [0268] A rock is a solid mass of geological material. In the present invention, the rock may be a source of metal cations. | [0269] Cations | [0270] Metal cations used in the method of the present invention include one or more of Mg2+, Ca2+. | [0271] Rock composition | [0272] According to the present invention, one or more rock types may be applied to soil, as is known in the technique of “enhanced weathering”. | [0273] In some embodiments, the rock comprises silica. In some embodiments, the rock comprises or consists of basalt. In some embodiments the rock comprises or consists of olivine. | [0274] In some embodiments, the rock comprises carbonates. In some embodiments, the rock comprises limestone. | [0275] Rock preparation | [0276] Prior to application to the soil, rocks that may be used in the method of the present invention may optionally be reduced in size, compared to an initial size, for example to increase rate of enhanced weathering. For example, a boulder may be reduced to a sand, or a pebble may be reduced to a powder or other particulate material typically less than e.g. 5mm or 1 mm diameter. In some embodiments, the rock is reduced in size by any one or combination of crushing, grinding, sieving, milling, pulverisation, and/or ball milling. | [0277] In some embodiments, the rock is particulate and has an average particle size of at least 1 micrometre. In some embodiments, the rock is particulate and has an average particle size of 5 millimetres or less. In some embodiments, the rock is particulate and has an average particle size of 4 millimetres or less. In some embodiments, the rock is particulate and has an average particle size of 1000 micrometres or less. In some embodiments, the rock is particulate and has an average particle size of 750 micrometres or less. In some embodiments, the rock is particulate and has an average particle size of 500 micrometres or less. In some embodiments, the rock is particulate and has an average particle size of 300 micrometres or less. In some embodiments, the rock is particulate and has an average particle size 1 micrometre to 300 micrometres. In some embodiments, the rock is particulate and has an average particle size of 400 micrometres or more. In some embodiments, the rock is particulate and has an average particle size of 500 micrometres or more. In some embodiments, the rock is particulate and has an average particle size of about 500 micrometres to about 4 millimetres. In some embodiments, the rock is particulate and hasan average particle size of about 500 micrometres to about 2000 micrometres, or about 500 micrometres to about 1500 micrometres, or about 500 micrometres to about 1000 micrometres, or about 500 micrometres to about 750 micrometres. Any appropriate method for determining particle size may be applied, as known in the art. One simple but effective method for sizing rock particles is sieve analysis, as is well known in the art. There are 2 types of sieve analysis that can be carried out: wet sieving and dry sieving. Wet sieving is suitable for particle sizes from 20pm up to 3mm while dry sieving is suitable for particles from 30pm up to 125mm. | [0278] In some embodiments, the rock is particulate and has an average particle size of at least about 500 micrometres to about 10 millimetres. In some embodiments, the rock is particulate and has an average particle size of at least about 500 micrometres to about 5 millimetres. In some embodiments, the rock is particulate and has an average particle size of at least about 0.5 millimetres to about 4 millimetres. In some embodiments, the rock is particulate and has an average particle size of at least about 500 micrometres to about 2 millimetres. In some embodiments, the rock is particulate and has an average particle size of at least about 500 micrometres to about 1 millimetre. | [0279] In some embodiments, the rock is reduced in size to a dust. In some embodiments, the rock is reduced in size to a powder. In some embodiments, the rock is reduced in size to particulates. In some embodiments, the rock is reduced in size to sand. | [0280] In some embodiments, the rock is applied to the soil as a dust or sand. In some embodiments, the rock is applied to the soil as a powder. In some embodiments, the rock is applied to the soil as particulate matter. | [0281] Application | [0282] Carbonic anhydrase and optionally rock are applied to soil in one aspect of a method of the present invention. | [0283] In some embodiments, the Carbonic Anhydrase and rock are applied to the soil simultaneously. Optionally, the Carbonic Anhydrase and rock are pre-formulated together prior to application, or are applied simultaneously from two or more different sources. Optionally, the Carbonic Anhydrase and rock are mixed together prior to application. | [0284] In some embodiments, the Carbonic Anhydrase and rock are applied to the soil contemporaneously. | [0285] In some embodiments, the Carbonic Anhydrase and rock are applied to the soil at different times. In some embodiments, the Carbonic Anhydrase and/or rock are applied to the soil two or more times, optionally two or more times in a day, a week, a month, a season, or a year.Frequency | [0286] In some embodiments, the Carbonic Anhydrase and/or rock is applied to the soil once a year. In some embodiments, the Carbonic Anhydrase and/or rock is applied to the soil twice or more a year. In some embodiments, the Carbonic Anhydrase and/or rock is applied to soil over one or more years. | [0287] In some embodiments, the Carbonic Anhydrase and/or rock is applied to the soil prior to planting crops. | [0288] Method | [0289] The Carbonic Anhydrase and/or the rock can be applied to the soil in different ways. | [0290] In some embodiments, the Carbonic Anhydrase and/or rock is sprayed onto soil. In some embodiments, the Carbonic Anhydrase and/or rock is spread onto soil. | [0291] In some embodiments, spreading can occur by hand. In some embodiments, spreading can occur by machine. In some embodiments, the spraying can occur by machine. In some embodiments, the Carbonic Anhydrase and/or rock can be dug into the soil, optionally by mixing and/or churning. | [0292] Typically, application will be done using machinery over one or more acres. In some embodiments, application will be done using machinery over ten or more acres, fifty or more aces, seventy or more acres, one hundred or more acres, two hundred or more acres, five hundred or more acres, one thousand or more acres, five thousand or more acres, ten thousand or more acres, twenty thousand or more acres. In some embodiments, application will be done using machinery over five or more hectares, ten or more hectares, fifty or more hectares, seventy or more hectares, one hundred or more hectares, two hundred or more hectares, five hundred or more hectares, one thousand or more hectares, five thousand or more hectares, ten thousand or more hectares. | [0293] Soil, Earth, Ground, Ocean | [0294] In some embodiments of the present invention, Carbonic Anhydrase and optionally rock are applied to soil. This attenuates, prevents, or reverses soil acidification. | [0295] In some embodiments, Carbonic Anhydrase and rock are applied to ground. The ground may or may not comprise soil. For example the ground may be scrubland or rocky ground. The ground may have plant cover, for examples grasses or trees. | [0296] In some embodiments, there is not substantial plant cover over the soil. Typically, the soil comprises or consists of bare soil. The rock and Carbonic Anhydrase can therefore directly contact the bare soil.Soil organic carbon (SOC) is the overall soil carbon content of a soil and may also be generally referred to as total organic carbon (TOC) (the terms may be used interchangeably), and this refers only to the carbon component of the organic matter in the soil. However, fluctuations in soil organic carbon may not necessarily correlate to the same fluctuations in stable soil carbon. Indeed, soils subjected to the treatments and methods may demonstrate minimal increases in TOC, but the percentage of said TOC that is captured in a stable form in the soil or in the fungi proliferating in the soil (i.e., complex polysaccharides, melanin, chitin, lignin, suberin and carotenoid compounds) may increase. The skilled addressee would also understand that changes in TOC and stable carbon in soil as a result of the treatments and methods of the present may take weeks, months or years, and therefore appropriate measurement timeframes must be applied. In one embodiment, the increase in soil organic carbon in a soil comprises an increase in stable carbon in the soil. | [0297] The soil carbon may be measured by methods including, but not limited to, dry combustion or elemental tests that may be analysed using, for example, the LECO analysis method, and loss on ignition (LOI) tests that may be analysed using the Walkley-Black method (see, for example, Walkley A, and Black IA (1934) An examination of the Degtjareff method for determining soil organic matter, and a proposed modification of the chromic acid titration method. Soil Science 37 , 29-38). To assess the prevalence of different types of carbon on the TOC (i.e. to measure the stable, or "recalcitrant" organic carbon), methods may be employed to fractionate to TOC by, for example, measuring soil respiration or the bulk density of the soil. | [0298] In some embodiments, the applying step comprises spraying the Carbonic Anhydrase onto the soil or ground. The Carbonic Anhydrase may be present in a slurry when sprayed, for example a fertilising slurry of the sort often used in agriculture. The slurry may comprise rock as described extensively herein. The Carbonic Anydrase, optionally in the form of a slurry, may be sprayed onto the soil or ground using agricultural equipment for example a spray bar or broadcast spreader. | [0299] While the disclosure focuses on solid ground, it can also be applied to large bodies of water such as in an ocean, sea or lake. All technologies of enhanced weathering where finely ground rock is deposited on or in an extensive area, e.g. farm, forest, ocean, lake or sea are contemplated within the scope of the invention. | [0300] Land | [0301] In some embodiments, the soil or ground is within agricultural land. In some embodiments, the soil or ground is within arable land. In some embodiments, the soil or ground is within pasture land.In some embodiments, the soil or ground is within pasture land. In some embodiments, the soil or ground is within waste land. In some embodiments, the soil or ground is within brownfield land. In some embodiments, the soil is within industrial land. | [0302] Depth | [0303] The present invention can advantageously retain Carbonic Anhydrase within a desired range of soil depth. | [0304] Typically, the Carbonic Anhydrase is retained in the top soil. Methods of measuring the depth of top soil are well known in the art. Typically, the depth of the top soil is measured downwards from the surface of the soil. | [0305] In some embodiments, the top soil extends 2 metres or less from the soil surface, and the Carbonic Anhydrase is retained in that region. In some embodiments, the top soil extends 1 metre or less from the soil surface. In some embodiments, the top soil extends 50 centimetres or less from the soil surface. In some embodiments, the top soil extends 30 centimetres or less from the soil surface. In some embodiments, the top soil extends 25 centimetres or less from the soil surface. In some embodiments, the top soil extends 20 centimetres or less from the soil surface. In some embodiments, the top soil extends 15 centimetres or less from the soil surface. In some embodiments, the top soil extends 10 centimetres or less from the soil surface. In some embodiments, the top soil extends 5 centimetres or less from the soil surface.| [0306] In some embodiments, the Carbonic Anhydrase is retained substantially on the surface of the top soil. For example, in some embodiments the Carbonic Anhydrase is retained in the top 5 cm of the soil, or the top 1 cm of the soil. In these embodiments, Carbonic Anhydrase remains exposed directly to the surface air and is not buried in the soil. | [0307] Increasing crop yield | [0308] In the present invention, Carbonic Anhydrase and optionally rock are applied to soil. The Carbonic Anhydrase may be applied to the soil in the form of being immobilised to a seed that is sown into the soil. The Carbonic Anhydrase may be applied to the soil in the form of being immobilised to a plant that is planted into the soil, optionally wherein the Carbonic Anhydrase is immobilised to the plant root. The seed coat and/or plant root may remain in the soil after the plant or a part of the plant is harvested, thereby also retaining the Carbonic Anhydrase in the soil. This attenuates, prevents, or reverses soil acidification, which can increase land productivity. In some embodiments of the invention, land productivity is increased after application of Carbonic Anhydrase and rock to soil. | [0309] For example, crop yields in the subsequent year or years can increase. In some embodiments, the crop yield obtained from land treated by application of Carbonic Anhydrase and optionallyrock to soil is increased by 5% or more compared to the previous crop yield from the same land. In some embodiments, crop yields are increased by 10% or more, 15% or more, 20% or more, 25% or more. | [0310] In other embodiments, the crop yield obtained from land treated by application of Carbonic Anhydrase and optionally rock to soil is increased by 5% or more compared to untreated land. In some embodiments, crop yields are increased by 10% or more, 15% or more, 20% or more, 25% or more. | [0311] The time taken to obtain increased crop yield can be over one or more years. In some embodiments, the crop yield is increased in the subsequent year to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased two years subsequent to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased three years subsequent to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased four years subsequent to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased five years subsequent to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased six years subsequent to the first application of Carbonic Anhydrase and rock to soil. | [0312] In some embodiments, the land retains higher productivity after application of Carbonic Anhydrase and rock to soil compared to untreated soil. | [0313] In some embodiments, the crop yields are higher in land treated by application of Carbonic Anhydrase and rock to soil compared to crop yields obtained from land treated by application of rock to soil alone. In some embodiments, the crop yields are higher in land treated by application of Carbonic Anhydrase and rock to soil compared to crop yields obtained from land not treated by application of carbonic anhydrase. | [0314] EMBODIMENTS | [0315] The disclosure further provides the following numbered embodiments as provided below, which are intended to define further the disclosed technologies but not intended to limit the scope of the invention. | [0316] 1. A method of sequestering atmospheric carbon, comprising the step of applying Carbonic Anhydrase and rock to soil. | [0317] 2. The method of embodiment 1 , wherein the Carbonic Anhydrase is immobilised to a solid support. | [0318] 3. The method of embodiment 2, wherein the solid support comprises or consists of:plant matter, optionally wherein the plant matter comprises or consists of corn husks and/or cellulose; and/or animal matter; and/or fibrous materials; and/or a bead; optionally wherein the solid support comprises or consists of waste material. | [0319] 4. The method of embodiment 2 or 3, wherein the solid support has a procurement cost of $20 or less per kg, $10 or less per kg, $5 or less per kg, $1 or less per kg, or $0.5 or less per kg. | [0320] 5. The method of embodiment 1 , wherein the Carbonic Anhydrase is immobilised to the rock, optionally directly to the rock, optionally by covalent bond or by non-covalent means such as physical adsorption. | [0321] 6. The method of any preceding embodiment, wherein the Carbonic Anhydrase has a structural modification to the enzyme which is intended to increase retention at a specified depth and/or location in the soil. | [0322] 7. The method of any preceding embodiment, wherein the Carbonic Anhydrase is retained in top soil; optionally wherein the top soil extends 1 metre or less from the soil surface, optionally 50 centimetres or less, 30 centimetres or less, 25 centimetres or less, 20 centimetres or less, 15 centimetres or less, or 10 centimetres or less. | [0323] 8. The method of any preceding embodiment, wherein the Carbonic Anhydrase is substantially retained at or around the roots of a plant, optionally in contact with one or more roots. | [0324] 9. The method of any preceding embodiment, wherein the soil is within: agricultural land, optionally wherein the agricultural land is arable land or pasture land; waste land; brownfield land; or industrial land. | [0325] 10. The method of any preceding embodiment, wherein the Carbonic Anhydrase and rock are applied to the soil simultaneously, contemporaneously or at different times.11. The method of any preceding embodiment, wherein the rock is a source of metal ions; optionally wherein the metal ions are cations, optionally wherein the cations are any of Mg+2 or Ca+2. | [0326] 12. The method of any preceding embodiment, wherein the rock comprises silica, optionally wherein the rock comprising silica is basalt or olivine. | [0327] 13. The method of any preceding embodiment, wherein the method comprises the step of reducing the rock in size before application to the soil, optionally wherein the rock is reduced in size by crushing, grinding, sieving, milling, pulverisation, and/or ball milling. | [0328] 14. The method of any preceding embodiment, wherein the rock is applied to the soil as a dust, powder, or particulate. | [0329] 15. The method of any preceding embodiment, wherein the Carbonic Anhydrase comprises an animal carbonic anhydrase, a plant carbonic anhydrase, and/or a bacterial carbonic anhydrase; optionally wherein the animal Carbonic Anhydrase comprises bovine erythrocyte carbonic anhydrase. | [0330] 16. The method of any preceding embodiment, wherein the Carbonic Anhydrase comprises an alpha, beta, delta, gamma, or zeta carbonic anhydrase. | [0331] 17. The method of any preceding embodiment, wherein the atmospheric carbon is sequestered as a carbonate, optionally as a magnesium carbonate or a calcium carbonate. | [0332] 18. A sequestered carbon obtained or obtainable by the method of any of embodiments 1 - 17. | [0333] 19. A mixture comprising Carbonic Anhydrase and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0334] 20. A mixture comprising Carbonic Anhydrase and rock, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0335] 21. A mixture comprising carbonic anhydrase, rock and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0336] 22. Use of a mixture according to any of embodiments 19 - 21 to sequester atmospheric carbon. | [0337] 23. A mixture according to any of embodiments 19 - 21 , for use in sequestering atmospheric carbon.24. A method of spraying an enzyme slurry or otherwise coating rock in a way that is compatible with agricultural equipment, e.g. a spray bar on a piece of broadcaster equipment. | [0338] 25. Carbonic anhydrase enzyme within a cell and bound to rock, such as via adsorption to rock particles of a cell that expresses Carbonic Anhydrase. | [0339] EXAMPLES | [0340] Summary: Carbon capture product to accelerate enhanced weathering. | [0341] Test suitability of commercially-available Carbonic Anhydrase (CA) enzyme for accelerated enhanced weathering using agriculturally acceptable solid carriers. Test activity and stability of the free enzyme under industrially relevant conditions (e.g. Temperature 4-20°C, ambient CO2, neutral and basic pH). Using commercial Carbonic Anhydrase enzyme, perform industrially relevant bead screens (e.g. basalt, vermiculite, perlite) for stability and activity. | [0342] Background. | [0343] - **Basalt.** In geology basalt reacts with CO2 from rain water to produce magnesium and calcium salts, such as, bicarbonate to store this mineral in the ground for millions of years. Basalt is mainly composed of SiO2 (45-52%), with CaO (5-10%), MgO (9.7%) and Na2<D (5.3%) plus many other metal oxides such as AI2O3 (13.1%) and Fe2Os (13.8%). [Basalt is negatively charged.] | [0344] - **Advanced weathering.** Accelerate this natural process by spreading raw and processed basalt on fields to capture and store CO2. | [0345] - **Carbonic anhydrase.** This is found in nature and converts CO2 and H2O into carbonic acid and protons, we want to utilise this enzyme to accelerate the advanced weathering phenomena by coating the enzymes directly on basalt rocks. It [converts 1 ,000,000 CO2 molecules per second]. This enzyme has been shown to bind to silica gel previously - see https://pubmed.ncbi.nlm.nih.gov/18584683/. | [0346] - **CO2 produced per year.** Across the world 93,000,000 barrels of oil are used per day (1 barrel = 200 L). CO2 emissions equate to 36.8 billion tonnes per year. We need to remove 1 billon tonnes per year to help slow down global warming.- **Alternative rocks.** Other rock types or minerals can also exhibit favourable properties for this application - see (https://en wikipedia.org/wiki/List of rock types). However most researchers are focused towards basalt. | [0347] - **Bead screen.** Initially we planned to perform a bead screen using a variety of agricultural beads, including basalt, vermiculite and perlite, plus and minus coating agents to improve stability. However looking into the feasibility of the project in more detail we realised it only makes sense to coat the enzyme directly onto basalt for the current application. Veolia have supplied two types of basalt, *raw* and *processed*. The latter is smaller and has a higher water content by around 30-40% v/w. | [0348] Key findings | [0349] CA from a commercial source is highly concentrated and active > Sigma Carbonic Anhydrase extracted from cows > bovine serum. | [0350] CA is able to turn over 4-nitrophenyl acetate or CO2. | [0351] CA is able to accelerate CO2 conversion using either NaCI, MgCI2, CaCI2 or basalt. | [0352] CA is able to bind and remain stable for up to 1 month at RT to either basalt, silica gel with or without fragmentation. | [0353] CA immobilised on basalt is stable and remains active over 4 uses. | [0354] CA from a commercial source loads 10 pL of enzyme onto 1 g of raw or processed basalt in 30 mins at RT in tap water. | [0355] Carbonic Anhydrase should be diluted down to 50L in tap water and then sprayed onto basalt directly on the field. | [0356] Carbonic Anhydrase can get washed off basalt rocks in soil so careful attention must be paid to how it interacts with soil. | [0357] Carbonic Anhydrase immobilised on silica gel is able to turn over CO2 and react with “sea water” in flow leading to a sea-based product. | [0358] Example 1 : Exemplary immobilisation soil test protocol | [0359] - Take 50L of 1x PBS buffer in a >50L container. Add the buffer reagent to the >50L container.| [0360] - Add 250g of Silica Gel | [0361] - Add 6g of enzyme | [0362] - Agitate/mix with a stirrer for 4hrs at room temp (25-30°C)- Apply directly to the soil as a wet solution. obtained from residual blood from meat| [0363] Bovine blood typically contains 7-15% w/v of CA. In this example, CA was obtained from residual blood from grocery store steaks, from Amazon and Sainsbury’s. In its unpasteurised form, milk contains CA. However, the pasteurisation process was expected to denature the majority, if not all, of the Carbonic Anhydrase. Therefore, pasteurised milk was used as a negative control in these experiments. | [0364] Method: 20 pL of blood solution was extracted from steaks obtained from Amazon and Sainsburys and placed into 180 pL water, then performed a 1 in 2 serial dilution. 10 pL of this liquid was used in a 4-nitrophenol acetate (4-NPA) assay. The 4-NPA assay involves the hydrolysis of 4-NPA by CA, and is described, for example in Shank et al. (2006) Chemical Biology & Drug Design 68(2)113-119. Specifically, 4-NPA, which is colourless, is hydrolysed to 4-nitrophenol (4-NP), which is yellow, and acetate. This colour change provides a spectrophotometric optical density readout. | [0365] Specifically, the 10 pL of and placed into 50 pL of 4-NPA mastermix in a 384-well plate. The absorbance was scanned at 400 and 500 nm. | [0366] Outcome: CA from both Amazon and Sainsbury’s was able to convert 4-NPA to 4-NP. As expected, pasteurised milk contained no active CA. Figure 1A shows outcome of the 4-NPA assay when serial dilutions of the blood solution obtained from the Amazon steak were used. Figure 1 B shows the product titre obtained from CA obtained from Amazon steak, Sainsbury’s steak, or pasteurised milk. | [0367] This example demonstrates that active CA can be obtained from an animal or part thereof, for example from the blood of the animal. | [0368] Example 3. CA obtained from animal blood has comparable activity to commercial CA. | [0369] This example shows that commercially-available CA, bovine serum, and blood from steak and minced beef show 4-NPA activity. | [0370] The 4-NPA assay described in Example 2 was repeated. Specifically, 1 mL of each CA source, underwent a 1 in 2 serial dilution, into a 96 deep well plate. Next, 10 pL of solution was added to 50 pL of 4-NPA mastermix in a 384-well plate. The profiles were plotted and the slopes generated. Figure 2A is a plot of activity slopes of the stated CA source assayed. Figure 2Bshows the activity kinetic plot of the buffer only, as negative control. Figure 2C shows activity kinetic plot for commercial CA with varying enzyme amount. Figure 2D shows activity kinetic plot for CA obtained from blood sample obtained from steak. Note, steak had a high background due to particle scattering, therefore the 5 pL plot was used to compare side-by- side. | [0371] Next, the thermal melting profile of the free enzymes was assessed. | [0372] Method: Commercial CA was diluted 1 in 5 into tap water, and steak blood was diluted 1 in 2 into tap water. The enzyme solution was transferred to 100 pL to 8x PCR tubes and heated at the stated temperature for 10 mins. Next, 10 pL of solution was added to 50 pL of 4-NPA mastermix in a 384-well plate and the 4-NPA assay as described in Example 2 was performed. The normalised profiles were plotted and the slopes generated. | [0373] Results: Figure 3 shows steak CA enzymes denature between 50 and 60 degrees, whilst the commercially-available CA did not unfold at all. | [0374] Example 4. Immobilising enzyme to different solid supports. | [0375] This example demonstrates that CA from various sources is able to bind and turn over product on sand, silica gel, chalk and dolomite. | [0376] Methods: 200 mg of the stated material was added to 100 pL of the stated crude enzyme. The enzyme was allowed to immobilise for 30 mins by shaking at 1250 r.p.m. at room temperature. The supports were washed by performing 5x wash-centrifugation cycles (except for the free enzyme controls which were not washed). Next, a 4-NPA activity assay was performed by adding 1 mL 4-NPA mastermix and shaking at 1250 r.p.m. for 30 minutes, isolating 50 pL of supernatant and transferring to a 384-well plate. The amount of product formed was plotted.| [0377] Results: Figure 4 shows CA from both sources was able to bind and turn over 4-NPA on sand, silica gel, chalk and dolomite. The commercial enzyme was added in about 5x excess, whilst the blood ratio was more efficient with almost quantitative loading. | [0378] Example 5. Carbonate formation. | [0379] This example demonstrates that CA obtained from bovine blood is able to capture and convert CO2 into sodium carbonate and or calcium carbonate using sea water.Method: 1 g of silica gel with or without 200 pL of Amazon CA was weighed out and placed in a 50 mL falcon tube and left to immobilise for 30 minutes. 10 mL sea water containing 1 M tris base at pH 10.5 was then added to control the pH shift. 1 mL of this mix was extracted and 100 pL of concentrated HCI was added. The falcon tube was heated to 50 degrees and 3x cardice (i.e., dry ice) cubes were added. After 10 minutes 1 mL was extracted and 100 pL of concentrated HCI was added. | [0380] Results: Figure 5 shows extensive bubble formation for CA obtained from bovine blood after the addition of cardice, indicating efficient CO2 capture and conversion to sodium carbonate or calcium carbonate. | [0381] Example 6 | [0382] In 6x 50 mL falcon tubes, either 0, 1 , or 10 mL of crude CA from a commercial source was added to 0.5 g of raw “R” or processed “P” basalt, supplemented with 0.1 M NaPi pH 7.0 (25 mL). All volumes were equal. Next, the falcon tubes were placed in a water bath set to 50 degrees, after 5 minutes single blocks of cardice were added and the colour change monitored. After 10 minutes, 50 pL was extracted and scanned the absorbance in a 384-well plate using the plate reader. | [0383] Pictures and absorbance profiles did not show the corresponding change in acid, potentially the basalt interacts with the indicator to corrupt the readout. Also, no apparent change in basalt mass was observed. | [0384] Figure 6 shows that bubbles formed when either raw “R” or processed “P” basalt was provided to the mix. | [0385] Example 7 | [0386] This example demonstrates that CA isolated from blood can be immobilised on CaCO3 and improve its thermal stability. | [0387] Method: 0.25mg of CaCO3 -/+ 200 uL of steak blood CA was added to a 1 .5 mL vial and left to immobilise for 30 minutes. The immobilised CA was then washed in water by performing 5x wash-centrifugation cycles. Next, the immobilised CA was moved into 100 uL PCR tubes and heated to the stated temperature for 10 minutes. Next, 100 uL of 4-NPA mastermix was added in a 384-well plate and mixed for 10 mins shaking at 1250 r.p.m., then extracted 50 uL supernatant. The absorbance was scanned. The normalised profiles were plotted and the slopes generated.Figure 7 shows CA can be stabilised on CaCO3 (chalk) and turn over 4-NPA product up to 60°C. | [0388] Overview of Examples 8 to 18 | [0389] The following examples show that the CO2 sequestration is effective for different sources of basalt. The use of a calcimeter provides a reproducible method for verification. | [0390] Example 8 | [0391] This example explains how measurements using a Calcimeter in subsequent examples were conducted. | [0392] Method: This analysis was performed using FOGL Bench-top Soil Calcimeter™ from bd Inventions. 5 g of sample was weighed into the sample container. 6 mL of 50% HCI (concentrated HCI diluted 1 :1 v/v using double distilled water) was added into the HCI container of the instrument. The sample weight was registered as 5 g and the measurement was initiated by pressing ‘start’ on the software. The lid was closed and all connections were ensured to be secure and airtight. The sample was mixed for 10 s and rested. The resulting change in partial pressure due to CO2 was measured by the instrument and reported as the %CO2 equivalents of CaCO3. | [0393] Example 9 | [0394] This example demonstrates free enzyme activity in water. | [0395] Method: 0.25 uL of a CA obtained commercially, 10 mL of water and 0.5 mL of 5 M CaCI2 were mixed. A negative control reaction was also set up, where water was used instead of enzyme. Each reaction was incubated at 60°C for 5 min in the water bath. Next, one block of equal sized dry ice was added into each tube and the experimentalist waited until the bubbling had stopped to close the tubes and incubate the tubes at 30°C for 5 min in a shaker, for the tubes were centrifuged for 5 min at 4,500 x rpm. The supernatant was decanted and the pellet was resuspended in 1 mL of ddH2O. The %CO2 for the 1 g sample was then measured using the Calcimeter. | [0396] Table 1 Variation of %CO2 equivalents for free enzyme reaction.No pellet had formed after the reaction, most likely because the dry ice added was not sufficient for the reaction to proceed within the limited time. | [0397] Example 10 | [0398] This example demonstrates the effect of buffer on the free enzyme reaction. | [0399] Method: 2 mL of a CA obtained commercially or, for negative control, buffer only, 10 mL of 1.5 M Tris-HCI pH 9.1 or 0.5 M Tris-HCI pH 8.5 (the experiment was performed using each type of buffer) and 0.5 mL of 5 M CaCI2 were mixed in a 50 mL Falcon tube. The tubes were then incubated in a water bath set to 60°C for 15 min in a fume hood. A small piece of dry ice was placed into each 50 mL Falcon tube. The reaction was allowed to proceed until the dry ice fumes stopped being released from the tubes. The tubes were incubate in the shaking incubator for 5 min (set to 37°C). The tubes were then centrifuged for 1 min at 4,300 x ref. The supernatant was decanted from the tubes. The pellets were resuspended in 1 mL of ddH2O. The calcimeter was set to measure 1 g of material; 1 mL of resuspended pellet from 2h was pipetted into the Calcimeter's Duran bottle and determine the carbonate content using the Calcimeter. | [0400] The outcome of the experiment is shown in Figure 8, where it was found that 1.5M Tris HCI buffer pH 9.1 is better for free carbonic anhydrase reaction. | [0401] Example 11 | [0402] This example demonstrates the effect of CaCI2 on free enzyme activity. | [0403] Method: Three tubes containing 0.25 uL of a commercially obtained CA and 10 mL of 1.5 M Tris pH 9.1 were set up. Either 0.1 mL of 5 M CaCI2 (Tube 1), 0.5 mL of 5 M CaCI2 (Tube 2) or 1 mL of 5 M CaCI2 (Tube 3) were added to each tube, which were then incubated at 60°C for 5 min in a water bath in a fume hood. One block of equal sized dry ice was added into each tube and the experimentalist waited until the bubbling had stopped before closing the tubes and incubating the tubes at 30°C for 5 min in the shaker. The tubes were then centrifuged for 5 min at 4,500 x rpm. The supernatant was decanted and the pellet was resuspended in 1 mL of ddH2O. The % CO2 for the 1 g sample was measured using the Calcimeter. | [0404] Table 2 Variation of %CO2 equivalents with CaCI2 concentration for free enzyme reaction.It was found 0.5 M CaCI2 was the optimum concentration to achieve the highest CO2 sequestration using free enzyme. | [0405] Example 12 | [0406] This example compares of carbonic anhydrase performance on Silica gel or basalt in buffered reaction. | [0407] Method: 1 mL of CA obtained commercially or ddH2O were mixed with 10 g of either Remin basalt (Rb), Duntilland basalt (Db) or 2.5 g of Silica gel (SG) in a 50 mL Falcon tube. 10 mL of 1.5 M Tris pH 9.1 buffer was added to each tube. The tubes were incubated on the rotor for 20 min at room temperature (RT). The immobilised CA was washed twice by adding 10 mL of ddH2O. 10 mL of 1.5 M Tris-HCI pH 9.1 and 0.5 mL of 5 M CaCI2 were added to the immobilised CAs. The tubes were incubated in the water bath set to 60°C for 15 min in the fume hood. A small piece of dry ice was added to each tube. The reaction was allowed to proceed until the dry ice fumes stopped being released from the tubes. The tubes were incubated in the shaking incubator for 5 min (set to 37°C). The tubes were then centrifuged for 1 min at 4,300 x ref. The supernatant was decanted from the tubes and the carbonate content was measured using the Calcimeter. | [0408] The outcome of the experiment is shown in Figure 9, which shows that Remin basalt (Rb) performed comparably to silica gel (SG) in terms of CO2 sequestration. | [0409] Example 13 | [0410] This example compares the effect of buffer and tap water on the CA reaction. | [0411] Method: 1 mL of CA obtained commercially was mixed with 10 g of either Remin basalt (Remin) or Duntilland basalt (Duntilland) or Tata steel slag (Steel slag) in a 50 mL Falcon tube. The Dentilland basalt and Tata steel slag both had particles with broad size up to 4000 micrometre. 10 mL of 1.5 M Tris pH 9.1 buffer was added to each tube. The tubes were incubated on a rotor for 20 min at room temperature (RT). The immobilised CA was washed twice by adding 10 mL of ddH2O. 10 mL of 1.5 M Tris-HCI pH 9.1 or 10-mL tap water was added to the immobilised CAs. 0.5 mL of 5 M CaCI2 was added to all the Falcon tubes. The tubes were incubated in the water bath set to 60°C for 15 min in the fume hood. A small piece of dry ice was added to each tube. The reaction was allowed to proceed until the dry ice fumes stopped being released from the tubes. The tubes were incubated in the shaking incubator for 5 min (set to 37°C). The tubes were centrifuged for 1 min at 4,300 x ref. The supernatant was decanted from the tubes and the carbonate content was measured using the Calcimeter.The outcome of the experiment is shown in Figure 10, which shows that tap water had considerable impact on CO2 sequestration. This is most likely due to the presence of divalent cations in the tap water, which are known to enhance carbonic anhydrase activity. Furthermore, steel slag was shown to have comparable performance to that of Remin basalt. | [0412] Example 14 | [0413] This example demonstrates onboarding of basalt sourced from Crag Mill. | [0414] Method: 1 mL of CA obtained commercially was mixed with 10 g of either Remin basalt (Remin) or Duntilland basalt (Duntilland) or Crag Mill basalt in a 50 mL Falcon tube. The Dentilland basalt and Crag Mill basalt both had particles with broad size up to4000 micrometre. 10 mL of tap water was added to each tube. The tubes were incubated on the rotor for 20 min at room temperature (RT). The immobilised CA was washed twice by adding 10 mL of tap water. 10 mL of tap water and 0.5 mL of 5 M CaCI2 were added to each tube. The tubes were incubated in the water bath set to 60°C for 15 min in the fume hood. A small piece of dry ice was added to each tube. The reaction was allowed to proceed until the dry ice fumes stopped being released from the tubes. The tubes were incubated in the shaking incubator for 5 min (set to 37°C). The tubes were then centrifuged for 1 min at 4,300 x ref. The supernatant was decanted from the tubes and the carbonate content was measured using the Calcimeter. | [0415] The outcome of the experiment is shown in Figure 11 , which shows that the absolute % CO2 equivalent captured using Crag Mill basalt is comparable to that captured using Dentilland basalt. However, the percentage improvement attained by adding enzymes to the basalt is highest at 125% compared to 67% and 7.5% for Remin basalt and Dentilland basalt, respectively. | [0416] Example 15 | [0417] This example demonstrates the effect of temperature, pressure, longer immobilization, and combination of increased pressure and temperature on the performance of CA immobilized on Dentilland basalt. | [0418] Method: 1 mL of CA obtained commercially was mixed with 10 g of Duntilland basalt (particle size up to 4000 micrometre) in each of 50 mL Falcon tubes 1 , 2, 3, and 4. 10 mL of tap water was added to each tube. T ubes 1 ,2, and 4 were incubated on the rotor for 20 min at RT, while tube 3 was incubated for 24 h. The immobilised CA was washed twice by adding 10 mL of tap water. 10 mL tap water and 0.5 mL of 5 M CaCI2 were added to the immobilised CAs. Each of the tubes were incubated in the water bath set to 60°C for 15 min in the fume hood. 2.5g of dry ice was added to each tube. The reaction was allowed to proceed until the dry ice fumesstopped being released from tubes 1 and 3. For tubes 2 and 4, dry ice fumes were trapped in the falcon to increase the pressure. Tubes 2 and 3 were incubated at 37°C, while tubes 1 and| [0419] 4 were incubated at 47°C for 5 minutes in a shaker incubator. The tubes were centrifuged for 1 min post reaction at 4,300 x ref. The supernatant was decanted from the tubes and the carbonate content was measured using the Calcimeter. | [0420] The outcome of the experiment is shown in Figure 12, which shows that the kinetic process conditions such as temperature, pressure did not influence the reaction performance of immobilized CA. Additionally, longer immobilization did not increase the enzyme loading or the CO2 capture. | [0421] Example 16 | [0422] This example demonstrates the effect of long-term CO2 exposure. | [0423] Method: 1 mL of CA obtained commercially or 1 mL water for control reaction was mixed with| [0424] 5 g of Duntilland basalt (particle size up to 4000 micrometre) in a 10 mL packed bed reactor. 10 mL of tap water was added to each reactor. The reactors were incubated for 60 min at room temperature (RT). CO2 gas was fed into the reactors for 23 h at 0.5 bars using a pressure regulator. To avoid dehydration by CO2, the CO2 was bubbled through water. The basalt was decanted into a clean Petri dish and the carbonate content was measured using the Calcimeter. | [0425] The outcome of this experiment is shown in Figure 13, which shows that the flow of CO2 increases the residence time and the mass transfer co-efficient. This improves the CO2 sequestration by 13x. | [0426] Example 17 | [0427] This example demonstrates immobilization efficiency and leaching of CA on Dentilland basalt. Method: 1 mL of CA obtained commercially was mixed with 10 g of Duntilland basalt in a 50 mL Falcon tube. 10 mL of tap water was added to the tube. The tube was incubated on the rotor for 20 min at room temperature (RT). The immobilised CA was washed twice by adding 10 mL of tap water. The supernatant post immobilization and the wash fractions were collected for later analysis. 10 mL of tap water and 0.5 mL of 5 M CaCI2 were added to the immobilised CAs. The reaction tube was incubated in the water bath set to 60°C for 15 min in the fume hood. 1g of dry ice was added to the tube. The reaction was allowed to proceed until the dry ice fumes stopped being released and the tube was incubated at 37°C for 5 minutes in a shaker incubator. After the reaction, the tube was centrifuged for 1 min post reaction at 4,300 x refand the supernatant fraction was collected. The enzyme activity of all the fractions was determined using 4-NPA assay and compared with the fresh enzyme of same dilution. | [0428] Carbonic anhydrase is bound to basalt using non-specific ionic interactions. The outcome of the experiment is shown in Figure 14. | [0429] Example 18 | [0430] This example demonstrates the results obtained from pre-trials in open field. | [0431] Method: Water permeable membrane was spread on grass land. 36 plots of 2m by 2m were measured and marked with ropes. 16 kg of Dentilland basalt or Remin basalt was added to 50 L water and the content was poured in the centre of the grid. The basalt was spread over the grid to form a layer. The bio-actives shown in Table 3 were sprayed at the required concentration of the respective grid. Samples were taken weekly on days on which precipitation did not occur. Approximately 50 g of basalt was scooped into a 50 mL falcon for sampling. The in situ pH probe was used to measure the pH in parallel during sampling. The residual enzyme activity was measured using the 4NPA assay and the carbonate content was measured using a Calcimeter. | [0432] Table 3 The different bio actives used in the pre-trial.| [0433] | [0434] The outcome of the experiment is shown in Figures 15A, 15B and 15C. | [0435] The pH measurements of the soil are shown in Table 3. These pH measurements were obtained when the soil temperature was 8.3°C, when there had been no precipitation for at least 24 hours, and were taken on day X12 after application of each CA source to the respective plot. Corresponding alpha, beta, gamma and delta plots, with Remin basalt, measured on day 12, were pH 6.2, 5.3, 6.2, and 5.9, respectively. The four control plots (without basalt and enzyme), measured on day 12, were pH 6, 6, 6.1 , and 6.2. | [0436] It was observed the CA obtained commercially along with Kefir, Yakult and baker’s yeast show relative increase in the CO2 equivalent measured using a Calcimeter, which indicated the presence of active CA and improved CO2 sequestration. | [0437] It is understood that the examples and embodiments described herein are for illustrative purposes only and that various modifications or changes in light thereof will be suggested to persons skilled in the art and are to be included within the spirit and purview of this application and scope of the appended claims. All publications, sequence accession numbers, patents, and patent applications cited herein are hereby incorporated by reference in their entirety for all purposes. (WO2024/201086)|[0001] METHOD OF SEQUESTERING ATMOSPHERIC CARBON | [0002] Field of the Invention | [0003] This invention relates to carbon sequestration, in particular by enhanced weathering. In particular, the invention relates to methods of sequestering atmospheric carbon by applying Carbonic Anhydrase, and optionally rock, to soil or earth. | [0004] Background of the Invention | [0005] Enhanced weathering sequesters carbon from carbon dioxide, accelerating the natural process of rock weathering. The application of finely-ground rock to agricultural land is one known method of utilising enhanced weathering to sequester atmospheric carbon. de Oliveira Maciel et al. (Chemosphere, July 2022, 299, 134419, 1-25) review the use of Carbonic Anhydrase to boost carbon dioxide sequestration. The authors note that Carbonic Anhydrase can be utilised in accelerated weathering. Ren et al. (Colloids and Surfaces B: Bioterfaces, August 2021 , 204, 111779, 1-10) review immobilisation of Carbonic Anhydrase and note the high cost of immobilisation supports. | [0006] There remains a need to improve methods of carbon sequestration, to address anthropogenic climate change and increase food security. | [0007] Summary of the Invention | [0008] The present disclosure relates in general to methods of carbon sequestration by enhanced weathering. The methods generally utilise an enzyme, typically carbonic anhydrase. In particular, the methods relate to application of an enzyme (such as carbonic anhydrase) and rock to soil, earth or ground. The methods also relate to contacting a plant or plant seed with Carbonic Anhydrase and then contacting that enzyme-inoculated plant material with the soil, i.e. by planting the seed or plant into the soil. Typically, this is carried out at large scale such a planting one or more fields with enzyme-inoculated seeds or plant material, or re-foresting an area with enzyme-inoculated tree roots. | [0009] This application of enzyme to a typically large area differs from “smokestack” carbon sequestration where carbon dioxide is removed from a chimney and where enzyme re-use and recycling is typically required. | [0010] The enzyme may be any enzyme that is capable of enhancing carbon sequestration into soil. The enzyme may be any enzyme that is capable of increasing plant yield.The enzyme may be any enzyme that is capable of capturing ambient carbon dioxide. | [0011] The enzyme is typically a carbonic anhydrase. Carbonic anhydrases are enzymes that convert carbon dioxide and water into bicarbonate and protons. | [0012] Enhanced weathering aims to accelerate the natural weathering of rock by spreading finely ground silicate rock, such as basalt, onto surfaces which speeds up chemical reactions between rocks, water, and air. It removes carbon dioxide (CO2) from the atmosphere, permanently storing it in solid carbonate minerals. | [0013] Enhanced weathering technology typically uses rock. This could include Olivine rock, Basalt, and other rocks rich in metal ions. The rock may be particulate. | [0014] Enhanced weathering projects have recently had MRV (Measurement Reporting, Verification) models accepted for carbon credits that can be sold commercially. Carbon credits are typically sold as carbon stored on a 20 year horizon. The MRV model is built around these timescales. Carbon sold at this price is currently charged at $200/ton of carbon sequestered from the ambient air. | [0015] Carbon credit duration can be securitized such that 1 year carbon sells for $800/ton and 20 year carbon sells for up to $200/ton. These prices come from present day demand shocks/high levels always being greater than prolonged carbon purchasing. If carbon sequestration projects could be accelerated than the total value from any project would be multiplied by 2x, 3x, 4x, or more. | [0016] Carbonic anhydrase is an enzyme that is widely known to produce carbonic acid from ambient CO2 and H2O. Carbonic Anhydrase is readily available at scale, studied extensively because of its prominence in natural systems as a pH regulator, and many commercial projects exist to try and sequester carbon using this enzyme. | [0017] Carbonic anhydrase can sometimes be very stable, but this depends on the host organism and enzymes from extremophile host organisms typically exhibit the highest stability to prolonged and continuous deactivation modes. | [0018] The Carbonic Anhydrase is typically immobilised to a solid support. The solid support may comprise or consist of rock, for example particulate rock such as basalt particles. The solid support may be a solid support that is separate from the rock, and which can be mixed with the rock. | [0019] In some embodiments, the solid support can be the rock, for example the particulate rock or rock sand. Accordingly, the disclosure provides immobilizing directly onto the ground rocks, e.g. finely ground rocks, via any binding chemistry and/or interaction. In some embodiments,the Carbonic Anhydrase is immobilised to the rock, optionally directly to the rock, optionally by covalent bond or by non-covalent means such as physical adsorption. | [0020] In some embodiments, cheap materials are used as the solid support for immobilisation to ensure commercial viability (e.g. waste solid supports and materials <$10, beneficially <$5, further beneficially <$1 kg, further beneficially <$0.5/kg). Examples of such materials include corn husks, waste cellulose, waste fibrous materials, typically farming additives used for liming such as vermiculite. | [0021] In some embodiments, the solid support is a plant seed. | [0022] In some embodiments the disclosure provides soil + finely ground rock + enzyme +/- immobilization. | [0023] In some embodiments the Carbonic Anhydrase enzyme is not immobilised, i.e. is a “free” enzyme. In some embodiments, the free enzyme binds to plant roots in the top soil or plant material above the top soil. | [0024] In some embodiments, the Carbonic Anhydrase enzyme is designed or engineered to accomplish retention at a specified soil depth with or without immobilisation, for example artificially making larger enzyme radius of gyration, and/or making enzyme charged so that it binds to plant roots at the optimal depth where CO2 is typically present at the roots. Accordingly, in some embodiments, the Carbonic Anhydrase enzyme is immobilised to the plant root. | [0025] Carbon can be introduced into the soil by the fixing of atmospheric carbon dioxide into plant biomass. The carbon in the plant biomass may then be converted into carbon dioxide by the respiration of organisms that aid the decomposition of the dead plant matter. Therefore, immobilising the enzyme to the plant root may be particularly beneficial, as this may bring the Carbonic Anhydrase enzyme in closer proximity to the organisms that aid the decomposition of the dead plant. In some embodiments, therefore, the solid support is a plant root or other part of a plant. | [0026] Carbon sequestration via enhanced weathering technology is readily scalable and almost profitable, but too slow to be economically attractive and impactful. The entire commercial value of enhanced weathering lies at the intersection of scale and speed. Scale is easy, speed has been elusive and comes with costs (e.g. grinding rock to be smaller and faster to react with naturally available carbonic acid, but the level of carbonic acid in soil is relatively low concentration and thus limiting on the rate of carbon sequestration). | [0027] In some embodiments, an increase in soil organic carbon comprises an increase in the level of stable carbon in the soil.In some embodiments, an increase in soil organic carbon comprises an increase in aggregate stability of the soil. | [0028] Typically, the “finely” ground rock particle sizes used in enhanced weathering are on the order of greater than 1 mm or even greater than 10 mm in diameter whereas enzymes are on the order of less than 10 nm in diameter. Enzymes are therefore much smaller, and as in reactor design around immobilized enzymes, this means that the enzyme is likely to leave the reaction environment before any chemical production is accomplished. | [0029] In some embodiments, the rock is particulate and has an average particle size of 50 micrometres or more, more typically 300 micrometres or more for example 500 micrometres or more. In some embodiments, the rock is particulate and has an average particle size of 5 millimetres or less. In some embodiments, the rock is particulate and has an average particle size of 4 millimetres or less. In some embodiments, the rock is particulate and has an average particle size of about 500 micrometres to about 5 millimetres micrometres. In some embodiments, the rock is particulate and has an average particle size of about 50 micrometres to about 4000 micrometres. In some embodiments, the rock is particulate and has an average particle size of about 500 micrometres to about 4000 micrometres. In some embodiments, the rock is particulate and has an average particle size of about 500 micrometres to about 2000 micrometres, or about 500 micrometres to about 1500 micrometres, or about 500 micrometres to about 1000 micrometres, or about 500 micrometres to about 750 micrometres. In some embodiments, the rock is particulate and has an average particle size of about 1 millimetre to about 4 millimetres, or about 2 millimetres to about 4 millimetres, or about 750 micrometres to about 4 millimetres, or about 750 micrometres to about 4.5 millimetres. In all of these embodiments, a typical rock is basalt. | [0030] In an improved method of enhanced weathering described herein, the enzyme stays close to the finely ground rock to help accelerate the carbon sequestration through local carbonic acid formation. The disclosed methods and compositions therefore resist the enzyme from being pushed deeper and deeper into the soil. | [0031] Enhanced weathering works effectively when ambient CO2 is brought down to the soil (or ground, or earth) by natural rainfall, although this could be extended artificially through techniques such as irrigation fields. When it rains and H2O brings CO2 to the Carbonic Anhydrase enzyme, carbonic acid forms, but also the enzyme tends to leach deeper into the soil because the enzyme is much smaller than the soil particle size and enzyme packing/residence time in the soil amongst the finely ground rock is vanishingly short. Thisdrives the whole application of enzymes to the enhanced weathering process to be technoeconomically unviable. | [0032] By increasing the surface area and particle size of the enzyme through immobilization onto a solid support biocatalyst, then the enzyme can be applied in economically efficient dosage to any enhanced weathering process and accelerate the carbon sequestration through prolonged proximity to the finely ground rock with charged metal ions. | [0033] Methods of the present invention are particularly advantageous as they utilise Carbonic Anhydrase in enhanced weathering applications to accelerate the ability of finely ground rocks to sequester carbon. The application of enzymes to finely ground rock for the purpose of enhanced weathering and carbon sequestration is beneficial. Advantageously, methods of the present invention bring about faster climate change impact from the same footprint and faster soil health recovery. Soil health may comprise increasing levels of organic soil matter, changing pH, and/or changing microbial growth patterns. | [0034] Certain aspects of the invention comprise one or more, for example all, of the following features: | [0035] 1 . An enzyme is selected to improve the enhanced weathering technology (in one of many technical and commercial ways). a. Specifically, the Carbonic Anhydrase enzyme rapidly accelerates the formation of carbonic acid in the soil and this is rapidly interacted with metal ions, optionally provided by the finely ground rock to accelerate the overall enhanced weathering. The metal ions may already be present in the soil. | [0036] 2. A solid support or solid support material may be selected for compatibility with the end field of use. The solid support may be a seed or a plant, or a rock. | [0037] 3. A binding chemistry or interaction is chosen for linking the enzyme to the solid support or solid support material. This can also selected for compatibility with the end field of use.| [0038] 4. The enzyme may be immobilized on the solid support or solid support material before application to the field of use. | [0039] 5. The enzyme can be pre-selected for compatibility with the solid support or solid support material and binding chemistry and/or interaction chosen. | [0040] 6. The immobilized enzyme is stabilized to prolonged continuous deactivation modes typically experienced for free enzymes (e.g. thermal).7. The immobilized enzyme is shielded from any deactivation and/or degradation due to protease activity because it is fastened to a much larger entity and restricting the protease from acting on the enzyme of interest. | [0041] 8. The immobilized enzyme is retained in the top soil being exposed to enhanced weathering technology (e.g. finely ground rock) due to the physical properties of the solid support (e.g. larger geometric size, charge, density) | [0042] 9. The solid support or solid support material is chosen to improve the top soil retention of the immobilized enzyme. | [0043] 10. The solid support or solid support material is chosen to promote the immobilized enzyme concentration/presence at a specified depth in the soil (e.g. might be nearer the roots of the natural plant organic matter). | [0044] 11. The solid support or solid support material is chosen to promote proximity to some element of the enhanced weathering process (e.g. finely ground rock, top soil plant organic matter, or anything else that might be deployed with the enhanced weathering technology)| [0045] In some aspects, natural (and/or unnatural) acids (and/or bases) can be created naturally (and/or unnaturally) in situ and react with the charged cation, a divalent metal cation and/or a monoatomic dication. | [0046] Brief Description of the Drawings | [0047] Figure 1A shows optical density readings from a 4-nitrophenyl acetate (4-NPA) assay performed using Carbonic Anhydrase (CA) obtained from bovine blood. The blood was obtained from Amazon steak meat. | [0048] Figure 1 B shows the product titre obtained from a 4-nitrophenyl acetate (4-NPA) assay performed using CA obtained from Amazon steak, Sainsbury’s steak, or pasteurised milk.| [0049] Figure 2A shows a plot of activity slopes of CA obtained commercially, bovine serum, blood obtained from Amazon steak, Sainsbury’s steak, or pasteurised milk. | [0050] Figure 2B shows an activity kinetic plot of the buffer used in Figure 2A only, as negative control.| [0051] Figure 2C shows an activity kinetic plot for CA at various dilutions. | [0052] Figure 2D shows an activity kinetic plot for CA obtained from blood obtained from Amazon steak meat. | [0053] Figure 3 shows a bar graph showing relative activity of commercially-obtained CA and CA obtained from blood obtained from Amazon steak meant at various temperatures.Figure 4 shows the product titre obtained from a 4-nitrophenyl acetate (4-NPA) assay performed using commercially-obtained CA or CA obtained from blood obtained from Amazon steak meat. Each CA was immobilised to different solid supports, namely sand, silica gel, calcium carbonate, or dolomite. | [0054] Figure 5 shows that CA obtained from blood obtained from steak immobilised to silica gel in sea water in acidic conditions is active. | [0055] Figure 6 shows 6x 50 mL falcon tubes containing either 0, 1 , or 10 mL of crude CA from a commercial source added to 0.5 g of raw “R” or processed “P” basalt, supplemented with 0.1 M NaPi pH 7.0 (25 mL). | [0056] Figure 7 shows a bar graph showing that CA obtained from animal blood immobilised on CaCO3 (chalk) can turn over 4-NPA product up to 60°C. | [0057] Figure 8 shows a bar graph showing CA-containing samples produced more CO2 compared to the buffer only controls. | [0058] Figure 9 shows a bar graph showing variation of measured %CO2 equivalents using different basalt carriers. Rb: Remin basalt; Db: Duntilland basalt; SG: silica gel. | [0059] Figure 10 shows a bar graph showing variation of measured %CO2 equivalents when using different basalt carriers and steel slag with tap water or buffer during the CA reaction. | [0060] Figure 11 shows a bar graph showing variation of measured %CO2 equivalents when using different basalt carriers, including basalt from Dentilland, Remin, and Crag Mill, with tap water during the CA reaction. | [0061] Figure 12 shows a bar graph showing the effect of different process conditions on CO2 capture by CA immobilised on Dentilland basalt performed in packed bed reactor, “w.r.t” means “with respect to”. | [0062] Figure 13 shows a bar graph showing the effect of CO2 gas flow on the CO2 capture by CA immobilised on Dentilland basalt performed in packed bed reactor, “w.r.t” means “with respect to”. | [0063] Figure 14 shows a bar graph showing the enzyme activity of supernatant (Sup after...), wash fractions (Wash 1 and Wash 2) and the supernatant after reaction (Sup after the reaction) were determined using 4NPA assay. | [0064] Figure 15A shows a bar graph showing variation of 4NPA activity of samples taken from the plots of the field pre-trial after 1 week and 2 weeks post-application of the CA source to the soil. The numbers on the x-axis denote plot numbers, which are provided in Table 3.Figure 15B shows a bar graph showing variation of CO2 equivalents of samples taken from the plots of the field pre-trials after 1 week and 2 weeks post-application of the CA source to the soil. The numbers on the x-axis denote plot numbers, which are provided in Table 3.| [0065] Figure 15C shows a bar graph showing percentage carbonate formation measured from samples taken from plots of the field pre-trials after 2, 4, and 6 weeks post-application of the CA source to the soil. | [0066] Detailed Description of the Invention | [0067] The disclosure is based on the development of new methods and compositions to sequester carbon in enhanced weathering by application of Carbonic Anhydrase, and optionally rock, to material such as soil or earth. This accelerates the rate of carbon sequestration. | [0068] In one aspect of the invention, Carbonic Anhydrase (and optionally rock) is applied to soil or earth. Advantageously, immobilisation of the Carbonic Anhydrase onto a solid support retains the Carbonic Anhydrase in the top soil. Similarly, engineering of the Carbonic Anhydrase to retain it at a defined soil depth is also advantageous. | [0069] Another aspect of the invention provides a mixture comprising Carbonic Anhydrase and seed, optionally wherein the Carbonic Anhydrase is immobilised to a solid support that may optionally be the seed. Another aspect of the invention provides a mixture comprising Carbonic Anhydrase and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0070] Another aspect of the invention provides a mixture comprising Carbonic Anhydrase and rock, optionally wherein the Carbonic Anhydrase is immobilised to a solid support that may optionally be the rock. | [0071] Another aspect of the invention provides a mixture comprising carbonic anhydrase, rock and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0072] Carbonic anhydrase enzymes are well-known in the art. This enzyme was first identified in 1933, in red blood cells of cows. Since then, it has been found to be abundant in all mammalian tissues, plants, algae and bacteria. This ancient enzyme has three distinct classes (called alpha, beta and gamma carbonic anhydrase). Members of these different classes share very little sequence or structural similarity, yet they all perform the same function and typically require a zinc ion at the active site. | [0073] PDB entries 1ca2 , 1ddz and 1thj are examples of the alpha, beta and gamma Carbonic Anhydrase enzymes, respectively.In some embodiments, the CA is from an animal species, for example cattle or sheep. | [0074] In some embodiments, the CA enzyme may be obtained, isolated or purified from animal blood, typically non-human mammalian blood, for example bovine or ovine blood. | [0075] In some embodiments, the CA enzyme may be produced recombinantly, typically expression of an exogenous gene in a host species. The host species is typically a microbial cell and/or the enzyme gene is expressed under a controllable promoter. For example, a mammalian carbonic anhydrase can be expressed in bacterial (e.g. E.Coli) or yeast (e.g. S.Cerevisiae or S.Pombe) cell, typically on a recombinant expression cassette. | [0076] Some aspects of the invention involve one or more of the following numbered features: | [0077] 1. Enzyme + solid support: identify pairing with retained enzyme activity and greatest imparted stability | [0078] 2. Select solid support to improve longevity of the accelerated enzyme effect on the pre- biologically treated version of enhanced weathering (whatever rock and/or system is being deployed) | [0079] 3. Select solid support to prevent leaching too deep into the soil, which is then too far from the enhanced weathering environment | [0080] 4. Select solid support to prevent deactivation and/or degradation by protease or other active entities in the environment of the enhanced weathering process. | [0081] Enzymes | [0082] The term enzyme is to be given its usual meaning in the art, i.e. a protein that accelerates or catalyses chemical reactions. An enzyme may have one or more active sites that bind to a substrate or selection of substrates. An enzyme may be naturally occurring or it may be of synthetic origin. | [0083] An enzyme is capable of catalysing a given reaction, and is sometimes thereof rereferred to as “an activity” or an “enzyme activity”. For example, a protein capable of catalysing the conversion of carbon dioxide and water into bicarbonate and protons is a Carbonic Anhydrase activity. | [0084] Suitable enzymes can include, for example: enzymes comprising natural and unnatural amino acids, chemical modifications or post-translational modifications; natural enzymes; wild-type enzymes; recombinant enzymes; enzymes produced by directed evolution, de novo design or the genetic fusion of peptide or protein domains; peptide catalysts; nucleic acid enzymes (e.g.ribozymes or DNA enzymes); hybrid catalysts; monomeric, dimeric or multimeric enzymes; enzymes produced in vivo or in vitro for example by solid-phase synthesis. | [0085] In an active enzyme system, the enzymes are provided under conditions suitable for enzyme activity, for example in the necessary physical and chemical conditions for enzyme activity. For the reaction to proceed, reagents will be needed, along with any necessary cofactor such as Zinc. Metal ions may also be included in the active enzyme system. | [0086] In the present invention, the enzyme is typically carbonic anhydrase. | [0087] In some embodiments, the Carbonic Anhydrase comprises an animal carbonic anhydrase. Optionally, the animal Carbonic Anhydrase comprises a mammalian carbonic anhydrase, optionally bovine erythrocyte Carbonic Anhydrase and/or human carbonic anhydrase. | [0088] In some embodiments, the Carbonic Anhydrase comprises a plant carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a bacterial carbonic anhydrase.| [0089] In some embodiments, the Carbonic Anhydrase comprises an alpha carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a beta carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a gamma carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a delta carbonic anhydrase. In some embodiments, the Carbonic Anhydrase comprises a zeta carbonic anhydrase. | [0090] In some embodiments, the Carbonic Anhydrase used in the method of the present invention comprises one or more classes of carbonic anhydrase. | [0091] Enzyme activity and stability | [0092] An enzyme in an active state, i.e. an active enzyme, is capable of catalysing a chemical reaction. | [0093] In one embodiment, an enzyme is stable if it remains in an active state for a period of time. In some embodiments, the period of time is at least a day, at least three days, at least 1 week, at least 2 weeks, at least 1 month, at least 6 weeks, at least 2 months, at least 3 months, at least 6 months, at least 9 months, at least 12 months, at least 18 months or at least 2 years, optionally wherein the period of time is at least one month or at least one year. | [0094] In some embodiments, the enzyme is active when present in soil as described herein, typically exposed to the elements and weather. | [0095] In some embodiments, the activity of an enzyme can be measured by the yield of the product produced by the enzymatic reaction, or by measuring conversion, depletion or consumption of the substrate. In some embodiments, the enzyme is active if the yield of product is about 40% or more, about 50% or more, about 60% or more, about 70% or more, about 80% or more,about 90% or more, or about 100% of the yield from the initial use cycle, when assessed under the same reaction conditions. | [0096] In some embodiments, the enzyme is stable over a given time period if, over that time period, the yield of product is about 40% or more, about 50% or more, about 60% or more, about 70% or more, about 80% or more, about 90% or more, or about 100% of the activity within one hour of immobilisation, when assessed under the same reaction conditions. | [0097] In some embodiments, the enzyme is active after 4 weeks or three months. In some embodiments, the enzyme is active over that time period if the yield of product is about 40% or more, about 50% or more, about 60% or more, about 70% or more, about 80% or more, about 90% or more, or about 100% of the activity within one hour of immobilisation, when assessed under the same reaction conditions. | [0098] In one aspect of the invention, a homologue of a reference enzyme has higher stability than the reference enzyme under the specified reaction process conditions. For example, a reference enzyme from a first species may catalyse a stated reaction when immobilised, but a homologue of that enzyme catalyses the same stated reaction with higher activity when immobilised to the same solid support. Typically, the homologue enzyme will have higher activity after a period of time, for example after weeks or months, and the long-term stable activity can be more valuable in terms of the efficiency of large scale biocatalysis than the initial activity shortly after immobilisation. Therefore, identifying homologues that are active and stable for a period of weeks, months or longer, is particularly advantageous. | [0099] Identification of one or more homologues | [0100] In one embodiment, an enzyme for immobilisation is identified by identifying two or more enzymes with different polypeptide sequences that catalyse a chemical reaction of interest. In some embodiments, the two or more enzymes comprises the enzyme of interest and one or more enzymes that are homologues of that enzyme of interest. In some embodiments, identifying the two or more enzymes is performed in a search, typically a search of one or more bioinformatic databases using one or mor bioinformatic search tools. | [0101] Bioinformatic databases and tools are well-known in the art. For example, a summary of useful bioinformatics tools can be found at www.ebi.ac.uk/tools and with sequence similarity searching tools collected at https://www.ebi.ac.uk/Tools/sss/ | [0102] In some embodiments, identifying the two or more enzymes is performed in a search wherein an amino acid sequence is an input. In some embodiments, identifying two or more enzymes is performed in a search wherein a nucleic acid sequence is an input. The input sequence is typically a reference enzyme sequence from a first species. In some embodiments, the search output is one or more amino acid sequences. In some embodiments, the search output is oneor more nucleic acid sequences. Typically, the search output includes an enzyme sequence from a different species from the reference sequence, that has a different sequence from the sequence of the reference enzyme, and that catalyses the same chemical reaction. | [0103] In some embodiments, the search comprises use of one or more sequence similarity searching methods. Optionally, the sequence similarity searching method is one or more of: BLAST (Basic Local Alignment Search Tool), optionally NCBI BLAST, PSI-BLAST, or PHI-BLAST; FASTA, optionally FASTA, SSEARCH, PSI-SEARCH, PSI-SEARCH2, GGSEARCH, GLSEARCH, or FASTM/S/F. | [0104] In some embodiments, the search comprises a classical literature search to identify additional mutations of the enzyme of interest. | [0105] In some embodiments, identifying the two or more enzymes comprises search which comprises one or more, optionally all, of use of one or more sequence similarity searching methods, alignment of multiple sequences, identifying an enzyme of interest and identifying sequences that are close to the enzyme of interest using a database of protein families, and identify additional mutations of the enzyme of interest. Optionally, two or more sequences are aligned again to remove redundancies. | [0106] Selection of one or more homologues | [0107] The present invention may involve the identification and selection of an enzyme and a solid support to which the enzyme can be immobilised. | [0108] In one aspect of the invention, the enzyme is identified by a method that comprises a step comprising identifying two or more enzymes with different polypeptide sequences that catalyse a chemical reaction of interest. In some embodiments, the two or more enzymes comprises one enzyme which is the enzyme of interest and one or more enzymes which are homologues of the enzyme of interest. | [0109] In some embodiments, properties of the one or more homologues are compared to properties of the enzyme of interest to select for one or more homologues for immobilisation. | [0110] Enzymatic activity is known to be influenced by factors including, but not limited to, temperature. Typically, the optimal temperature for an enzyme is the temperature which allows the enzyme to function at maximal activity. | [0111] In some embodiments, the enzyme is derived from a mesophilic organism. In some embodiments, the enzyme is derived from a cryophilic organism. | [0112] In some embodiments, the enzyme or homologue is mesophilic. In some embodiments, the enzyme or homologue is cryophilic.In some embodiments, the optimum temperature of the enzyme or homologue is 70°C or less, for example between 40°C and 70°C . In some embodiments, the optimum temperature of the enzyme or homologue is 50°C or less, for example between 40°C and 50°C. In some embodiments, the optimum temperature of the enzyme or homologue is 40°C or less, for example between 30°C and 40°C. In some embodiments, the optimum temperature of the enzyme or homologue is 30°C or less, for example between 20°C and 30°C. In some embodiments, the optimum temperature of the enzyme or homologue is 20°C or less, for example between 10°C and 20°C. In some embodiments, the optimum temperature of the enzyme or homologue is 15°C or less, for example between 5°C and 15°C. In some embodiments, the optimum temperature of the enzyme or homologue is 5°C or less, for example between minus 20°C and plus 5°C or between minus 20°C and 0°C. | [0113] In a further embodiment, such enzymes or homologues are engineered to improve their stability. | [0114] Selection of enzyme or homologue according to temperature of geographical region| [0115] Enzymatic activity is known to be influenced by factors including, but not limited to, temperature. Typically, the optimal temperature for an enzyme is the temperature which allows the enzyme to function at maximal activity. | [0116] The present invention may involve the identification and selection of an enzyme according to the temperature of the geographical location or region to which the enzyme is to be applied. The selection of the enzyme may be determined according to one or more of previous temperature recordings, current temperature recordings, and predictions of future temperature. In some embodiments, the temperature comprises or consists of the temperature of air. In some embodiments, the temperature comprises or consists of the temperature of top soil. In some embodiments, the temperature comprises or consists of the average temperature of the geographical location or region. In some embodiments, the average temperature comprises or consists of a yearly average. In some embodiments, the average temperature comprises or consists of the average temperature over the course of a growing season of a crop. In some embodiments, the average temperature comprises or consists of the day average temperature. In some embodiments, the average temperature comprises or consists of the night average temperature. In some embodiments, the average temperature comprises or consists of the day average temperature and the night average temperature. | [0117] Typically, methods of sequestering carbon according to the present invention may occur in geographical locations or regions where the average temperature is about 70°C or less. Accordingly, an enzyme or homologue that has an optimal activity at a temperature of about 70°C or less may be selected. In some embodiments, the optimal activity of the enzyme orhomologue occurs at 70°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at60°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 50°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at40°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 30°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at20°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 15°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 10°C or less. In some embodiments, the optimal activity of the enzyme or homologue occurs at 5°C or less. | [0118] Different homologues may be selected for use in a method of sequestering carbon according to the present invention, depending on the geographical location. For example, a homologue with a lower optimal temperature may be preferentially selected for use in a colder geographical location than a warmer geographical location. | [0119] Accordingly, in some embodiments, the optimal temperature for the enzymatic activity of an enzyme or homologue corresponds to the average temperature of the geographical location or region to which the enzyme is applied or will be applied. In some embodiments, the optimal temperature is within 20°C of the average temperature of the geographical location or region. For example, if the average temperature of the geographical location or region is 20°C, the optimal temperature for enzyme activity would fall between 0°C and 40°C. In some embodiments, the optimal temperature is within 15°C of the average temperature of the geographical location or region. In some embodiments, the optimal temperature is within 10°C of the average temperature of the geographical location or region. In some embodiments, the optimal temperature is within 5°C of the average temperature of the geographical location or region. | [0120] Cells comprising carbonic anhydrase | [0121] The disclosure typically contemplates the use of an isolated, purified or partly-purified carbonic anhydrase enzyme, for example that has been extracted from its natural environment by an isolation or purification process. This may be purification such that the carbonic anhydrase is the majority component, or substantially the only component, of a preparation following a purification step (e.g. the enzyme has been purified using one or more chromatography steps as are well-known in the art). The enzyme may alternatively have been only slightly isolated from the cell in which it was expressed, for example the enzyme can be provided in a lysate.In some embodiments the enzyme is not separated from the cell in which it is expressed. The carbonic anhydrase is applied to the soil while still inside a cell, i.e. a cell comprising the enzyme is applied to the soil. The cell may be alive or dead. The cell should contain carbonic anhydrase protein, and/or have the function of being able to express carbonic anhydrase under appropriate conditions. This ability requires the presence of a nucleic acid sequence that encodes a carbonic anhydrase enzyme. The carbonic anhydrase may be endogenous to the cell, or may be exogenous (e.g. expressed recombinantly). | [0122] Typically, the cell is a microorganism. In this aspect of the invention, a method of sequestering atmospheric carbon comprises the step of applying a microbe and optionally rock to soil, wherein the microbe expresses (or has previously expressed, or is able to express) carbonic anhydrase. Typically, the microbe endogenously expresses carbonic anhydrase. | [0123] The microbe typically comprises one or more single-celled organisms, optionally a prokaryotic cell, a fungal cell, a microalgae cell, an archaea cell, and/or a bacterial cell. | [0124] In some embodiments, the microbe: is obtained from or is present in milk, fermented milk, yogurt or kefir; comprises or consists of lactobacillus, lactococcus, leuconostoc, streptococcus or enterococcus bacteria; comprises or consists of Saccharmocyes Cerevisiae, baker’s yeast, brewer’s yeast or Schizosaccharomyces pombe', comprises or consists of compost starter containing organisms; comprises or consists of a combination of at least one bacterium and at least one fungus, optionally wherein the at least one bacterium comprises an Actinomycetes. | [0125] Table 3 in the Examples below demonstrates the use of carbonic-anhydrase expressing cells from a wide range of sources, including chicken serum, potatoes, bakers’ yeast, brewers’ yeast, compost starter, yogurt (comprising Lacticaseibacillus casei Shirota), eggs, raw goats milk, beef, pork, raw cows milk and grass. Each of these sources of CA is provided as a separate embodiment of the invention. These cells themselves can be used according to the present disclosure, or the enzyme can be extracted, isolated or purified and used as a purified enzyme preparation or a part-purified extract.In some embodiments, the cell comprising carbonic anhydrase may be immobilised to rock, typically particulate rock. Any technique of immobilising the cell to the rock can be used, for example adsorption. | [0126] Immobilised enzymes | [0127] Compared to free enzymes in solution, immobilised enzymes are typically more robust and more resistant to environmental changes. | [0128] Multiple copies of a single enzyme may be attached to a single support, for example a single bead or other solid support as described herein e.g. waste material such as a corn husk or fragment thereof, the rock component itself, a seed, or a plant. These may be attached in an identical fashion, or different copies of a single functional molecule may be attached differently. This can provide, for example, improved activity for a single type of functional molecule when the structure is placed under different bulk environmental conditions. | [0129] In some embodiments, two or more different Carbonic Anhydrase enzymes (i.e. different sequences) are attached to each support, e.g. each bead, each rock particle, each seed, or each plant. These may each be present once, or may each be present multiple times. | [0130] Solid Supports | [0131] The invention typically involves immobilising an enzyme, typically Carbonic Anhydrase, to a solid support. The solid support may comprise controlled pore glass, polystyrene, sepharose or alginate. In some embodiments, the solid support is particulate. The solid support may comprise beads, for example, controlled pore glass beads, polystyrene beads or buoyant beads. In some embodiments, the solid support is a resin. In some embodiments, the solid support is magnetic, for example magnetic beads. In one embodiment, the solid support comprises Poly(styrene-divinylbenzene). | [0132] Typically, the solid support is available at a low cost to ensure commercial viability of the method. | [0133] In some embodiments, the enzyme is directly immobilised onto the rock, e.g. finely ground rock, used for the enhanced weathering process. | [0134] Plants and seeds as solid supports | [0135] Without wishing to be bound by theory, the inventors have found that inoculating an enzyme such as Carbonic Anhydrase onto a plant seed or plant root has many advantages over microbial inoculations, including one or more of: | [0136] - the enzyme is easier to scale than the microbial inoculant in an expression vessel.- the enzyme dosing onto the seed or plant can be controlled much more easily than inoculated microbial systems in the soil | [0137] - the enzyme might be more efficient than other related microbial approaches at helping to sequester carbon for agricultural fields | [0138] - the enzyme can be modified for improved properties and still considered non-GMO compared to the microbial inoculant. | [0139] The inventors also consider, without being bound by theory, that the enzyme might be more active deeper in the soil near the plant roots where biomass decomposition leads to enhanced CO2 levels. | [0140] Notably, rock such as basalt is not required for Carbonic Anhydrase enzyme to be inoculated on seeds or plant. The salinity + CO2 + water in the soil is suitable to carry out the carbon sequestration. Rock may be added in some embodiments. | [0141] In certain embodiments, the plant or seed is sprayed with a liquid comprising the enzyme, wherein the enzyme is typically carbonic anhydrase. Methods of spraying plants and plant seeds are known in the art. | [0142] Seed as a solid support | [0143] In one aspect the solid support is a seed. In some embodiments, the enzyme is immobilised onto a seed. Typically, the seed is a variety used in agriculture. In some embodiments, the enzyme is directly immobilised onto the seed. In some embodiments, the enzyme is directly immobilised onto the seed coat. | [0144] Certain non-limiting aspects and embodiments relate to coating, dipping or spraying agricultural seeds with a liquid containing Carbonic Anhydrase enzyme, which then achieves immobilization of the enzyme onto the hard shell of the seed before it is placed in the soil. The Carbonic Anhydrase enzyme then remains in/around the plant root system for a prolonged period of time, for example one month or more. | [0145] Typically, the enzyme is immobilised onto the seed before the seed is sown. Accordingly, in some embodiments, the seed is contacted with a mixture comprising the enzyme, typically a liquid mixture. In some embodiments, the seed is sprayed with the mixture. In some embodiments, the seed is stirred with or into the mixture. In some embodiments, the seed is introduced to the mixture and the mixture is aerated. In some embodiments, the seed is submerged in the mixture. In some embodiments, the seed is placed on an article comprising the mixture. In some embodiments, the seed is placed within an article comprising the mixture. In some embodiments, the seed is placed underneath an article comprising the mixture. In some embodiments, the seed is placed on an article soaked in the mixture. In someembodiments, the seed is placed within an article soaked in the mixture. In some embodiments, the seed is placed underneath an article soaked in the mixture. Following contact with a liquid comprising the enzyme, the seed is typically removed from contact with the enzyme liquid, and may optionally be allowed to dry in ambient surroundings or be subjected to an active drying step. | [0146] Some agricultural crop seeds undergo seed priming prior to sowing. Seed priming is a process of regulating the germination process by managing the temperature and seed moisture content. In some embodiments, the seed is contacted with the enzyme (e.g. mixture comprising the enzyme) prior to priming. In some embodiments, the seed is contacted with the mixture during priming. In some embodiments, the seed is contacted with the mixture after priming. | [0147] Accordingly, the present disclosure provides a mixture comprising Carbonic Anhydrase and seed, wherein the Carbonic Anhydrase is immobilised to the seed. In some embodiments, the mixture is sown into agricultural land. | [0148] Immobilising the enzyme to a seed coat may be particularly useful commercially, as this may allow for reduced labour time on agricultural land and/or reduce the need for additional steps to supply the enzyme to the top soil separately to the seed. | [0149] Plant as a solid support | [0150] In another aspect, the solid support is a plant. Typically, the plant is suitable for growing as an agricultural crop. In some embodiments, the enzyme is directly immobilised onto the plant. The enzyme may be immobilised onto one or more parts of the plant, including but not limited to, the plant root, the plant stem, the plant leaf, the plant bulb, and the plant tuber. In some embodiments, the enzyme is directly immobilised onto the plant stem. In some embodiments, the enzyme is directly immobilised onto the plant bulb. In a further embodiment, the enzyme is directly immobilised onto the bulb tunic. In some embodiments, the enzyme is directly immobilised onto the plant tuber. In some embodiments, the enzyme is directly immobilised onto the plant tuberous root. In a further embodiment, the enzyme is directly immobilised onto the tuber periderm. In a preferable embodiment, the enzyme is directly immobilised onto the plant root. In some embodiments, the plant is a seedling. In some embodiments, the plant is a mature plant. | [0151] The enzyme may be immobilised onto the plant before it is planted in agricultural land. Accordingly, in some embodiments, the plant is contacted with a mixture comprising the enzyme. In some embodiments, the plant is sprayed with the mixture. In some embodiments, the plant is dipped into the mixture. In some embodiments, the plant is submerged in the mixture. In some embodiments, the plant is watered with the mixture. For example, the enzymemay be immobilised onto the plant root by contacting the plant root with a mixture comprising the enzyme, optionally wherein the contacting occurs by one or more of spraying, dipping, submerging, and watering. | [0152] The enzyme may be immobilised onto the plant after it is planted in agricultural land. Accordingly, in some embodiments, the plant is contacted with a mixture comprising the enzyme. In some embodiments, the plant is sprayed with the mixture. In some embodiments, the plant is watered with the mixture. In some embodiments, the mixture is provided to the plant through an irrigation system. For example, the enzyme may be immobilised onto the plant root by contacting the plant root with a mixture comprising the enzyme, optionally wherein the contacting occurs by watering the plant with the mixture, optionally wherein the watering is performed using an irrigation system. | [0153] Species of plants and seeds | [0154] In some embodiments, the plant or seed is a crop plant or crop plant seed, optionally a crop plant of agronomic importance which is cultivated for food, animal feed, fiber, fuel, and/or industrial purposes. In one embodiment, the crop plant is a commercial crop plant. A commercial crop plant is a plant cultivated to produce a harvested horticultural product that is for sale and/or profit, as well as subsistence crops which may be grown to support other agricultural products, such as livestock. | [0155] In one embodiment, the plant is a commercial crop plant. In one embodiment, the commercial crop plant is a compatible crop selected from the group consisting of species of the genus Triticum, Brassica, Gossypium, Zea, Corchorus, Saccharum, Medicago, Lolium, Coffea, Camellia, Oryza, Hordeum, Boehmeria, Nicotiana and Cannabis. | [0156] In one embodiment, the commercial crop is selected from the group consisting of the species Triticum aestivum, Brassica napus, Brassica rapa, Brassica juncea, Gossypium hirsutum, Gossypium barbadense, Gossypium arboretum, Gossypium Herbaceum, Zea mays, Medicago sativa, Lolium multiflorum, Corchorus capsularis, Saccharum officinarum, Cannabis sativa, Coffea Arabica, Coffea Robusta, Camellia sinensis, Oryza sativa, Hordeum vulgare, Boehmeria nivea and Nicotiana tabacum. | [0157] In one embodiment, the crop plant is a cereal plant. Cereal plants include, for example, wheat [Triticum), rice [Oryza), barley [Hordeum), corn [Zea). | [0158] In one embodiment, the cereal plant is selected from wheat, and barley. | [0159] In one embodiment, the cereal plant is a wheat plant. | [0160] The inventors have found that growing a plant or seed that has been contacted with an enzyme such as Carbonic Anhydrase results in an increase in soil carbon and/or an increase in yieldof the plant being cultivated in the soil. The plants may be crop plants, which are known in the art and include for example wheat, canola, and barley. Applying the enzyme to the plant or seed can result in increased yield of plant relative to untreated plants. The inventors have further found that the soil in which these plants are grown can have increased organic carbon content relative to soil in which untreated plants are grown. | [0161] In some embodiments, the present disclosure to enhancement of agricultural soils, mitigating atmospheric carbon dioxide, and providing agronomic benefits to crop plants. Additionally, the present disclosure relates in part to methods and compositions for increasing soil organic carbon in soil, and increasing crop plant yield. | [0162] In some embodiments, the soil is contacted with the enzyme. The soil may be contacted with the enzyme prior to planting a plant, for example before, during, or after tilling the soil in preparation for planting. In other embodiments, the soil may be contacted with the enzyme after the plant has been planted. In some embodiments, the soil is contacted with the enzyme by planting in the soil plants that have been contacted with the enzyme. | [0163] In some embodiments, the step of contacting with the enzyme comprises applying the enzyme to seeds of the plant prior to planting. | [0164] In some embodiments, the step of contacting with the enzyme comprises applying the enzyme to seedlings of the plant. | [0165] In some embodiments, the step of contacting with the enzyme comprises applying the enzyme to a plot of soil that is cultivated, such that the enzyme is retained by the soil as the crops are rotated, even in the absence of crops for periods of time. | [0166] In one embodiment, the plants are contacted with the enzyme as a seed coating before, during or after one or more of the stages of germination of a seed, or as a root inoculant of a seedling. For example, the enzyme may be applied as a seed coating to seeds at large scale prior to sowing a crop. | [0167] In some embodiments, the enzyme is provided as a composition comprising an agriculturally acceptable excipient. | [0168] As used herein, an "agriculturally acceptable excipient" refers to an essentially inert substance that can be used as a diluent and/or carrier for the enzyme and is not detrimental to the plant or seed. | [0169] In one embodiment, the agriculturally acceptable excipient is a solid or liquid carrier. Suitable solid carriers include mineral earths (e.g., calcium phosphate, calk, clay, diatomaceous earth, dolomite, kaolin, silicates, silica gels, talc, etc), cellulose, and starch. Suitable liquid carriers include water, or any other liquid solvents which are not toxic to the seed or the plant.In one embodiment, the composition comprises an agriculturally acceptable additive. As used herein, an "agriculturally acceptable additive" is an additive that may assist in or enhance the performance of the enzyme and/or the plant or seed, and is not detrimental to the one or more enzyme or to the plant or seed. Examples of agriculturally acceptable additives include preservatives, stabilizers, nutrition enhancers, wetter-spreaders, stickers (adhesives), penetrants, root promoters, fungicides, urea, fertilisers, pesticides, fulvic acid, humus, nanoparticles/nanomaterials. | [0170] In some embodiments, the enzyme may be provided as a composition in the form of a dried powder, a spray, a slurry, a sachet, a liquid, a jelly, a seed coating, an enhancer, and/or combinations thereof. In some embodiments, the composition is in the form of a seed coating, a foliar spray, granule, powder, soil drench or a root dip. | [0171] In some embodiments, the composition is in the form of a seed coating. | [0172] In some embodiments, the composition is in the form of a foliar spray. | [0173] In some embodiments, the composition is in the form of a soil drench. | [0174] In some embodiments, the composition is in the form of a root dip. | [0175] Solid support cost | [0176] The invention typically utilises solid supports that are available at a low cost to ensure commercial viability of the method when applied at a large scale, for example to be spread over acres or hectares of ground. | [0177] In some embodiments, the solid support has a procurement cost of $20 or less per kg. Typically, the solid support has a procurement cost of $10 or less per kg. It is beneficial if the solid support has a procurement cost of $5 or less per kg and beneficial further still if the solid support has a procurement cost of $1 or less per kg, or $0.5 or less per kg. | [0178] Source of alternative solid supports | [0179] In some embodiments, the solid support comprises plant matter. In some embodiments, the plant matter comprises vegetable matter, optionally fibrous matter. In some embodiments the vegetable matter comprises waste matter from the farming process and/or food chain. In some embodiments, the waste matter comprises corn husks. | [0180] In some embodiments, the solid support comprises animal matter, optionally fibrous matter.| [0181] Typically, the solid support is obtained from waste matter. In some embodiments, the waste matter comprises or consists of produce such as fruit and/or vegetables (e.g. corn or corn husks) that are too old, spoiled or rotten to be sold, or are inedible. In some embodiments, the waste matter comprises fibrous plant or animal matter that is too old, spoiled or rotten to besold, or is inedible. In certain embodiments, the solid support is from material that would otherwise be seen as low or no value, or as a waste product. In some embodiments, the solid support is from commercial waste or household waste. | [0182] Typically, the material is robust enough not to degrade significantly, or at all, over a period of at least 6 months, or least one year. | [0183] Bead solid supports | [0184] In some embodiments, the solid support is a bead. Solid supports that are beads are well- known in the art. In some embodiments, the solid support is a resin bead. Resin beads are well-known in the art. Resin beads are typically essentially spherical. | [0185] In some embodiments, the bead is porous. In porous beads, binding sites can also be internal, leading to higher loading of enzyme. | [0186] The beads may be from 10 micron to 1500 micron diameter, typically 100 micron to 1200 micron, for example 150 micron to 300 micron diameter. | [0187] In some embodiments, the beads are methacrylate beads, for example epoxy methacrylate beads, epoxy/butyl methacrylate beads, amino C2 methacrylate beads or Amino C6 methacrylate beads. | [0188] The inventors have successfully immobilised enzymes using a variety of beads including amine-functionalised beads and epoxy-functionalised beads. | [0189] Epoxy resins | [0190] Beads that are functionalised with epoxides are known as “epoxy” functionalised resins, or epoxy-resins. The IIIPAC name for an epoxide group is an oxirane. Epoxides react with nucleophiles and in the context of protein immobilisation, the reactive residues will typically be Lys and Cys (and sometimes His). Surface epoxy groups on beads therefore allow direct covalent binding of proteins or peptides, which can be achieved by simple incubation of the protein or peptide with the epoxy-bead, for example overnight. | [0191] Epoxy-functionalised beads can be used in the invention because they form very stable covalent linkages. | [0192] In some embodiments, the bead is an epoxy-methacrylate bead. In some embodiments, the bead is an epoxy/butyl methacrylate bead. | [0193] In some embodiments, the pore diameter of the epoxy beads is 300 to 1800 A. Optionally, the pore diameter is 300 to 600 A, 450 to 600 A, or 1200 to 1800 A. In some embodiments, the total moisture of the beads is 50 to 80%. | [0194] Optionally, the total moisture of the beads is 50 to 65%, or 70 to 80%.In some embodiments, a minimum of 85% of the beads are perfectly spherical. Optionally a minimum of 95% of the beads are perfectly spherical. | [0195] In one embodiment, the epoxy beads are epoxy/butyl methacrylate beads, wherein the particle size range is 250 to 1000 micron, the pore diameter is 450 to 650 A, and the total moisture is 70 to 80%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage at 2 to 8°C. Optionally, a minimum of 85% of the beads are perfectly spherical. | [0196] In one embodiment, the epoxy beads are epoxy methacrylate beads, wherein the particle size range is 150 to 300 micron, the pore diameter is 300 to 600 A, and the total moisture is 50- 65%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage from 2 to 8°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0197] In one embodiment, the epoxy beads are epoxy methacrylate, wherein the particle size range is 150 to 300 micron, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage at 2 to 8°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0198] Amine-functionalised resins | [0199] Beads that are functionalised with amines are known as amine-functionalised beads or amine- functionalised resins. Amine functional groups form covalent amide bonds with proteins or polypeptides. Amine-functionalised beads are generally pre-activated with glutaraldehyde, prior to ionic polypeptide immobilisation. pH adjustment during incubation results in the formation of an amide bond between the bead and the protein or polypeptide. | [0200] In some embodiments, the bead is an amino C2 methacrylate bead. In some embodiments, the bead is an amino C6 methacrylate bead. | [0201] In some embodiments, the particle size range of the amine-functionalised beads is 150 to 300 micron. | [0202] In some embodiments, the pore diameter is 600 to 1800 A. Optionally, the pore diameter is 600 to 1200 A, or 1200 to 1800 A. | [0203] In some embodiments, the total moisture of the beads is 62 to 80%. Optionally, the total moisture is 62 to 72%, or 70 to 80%. | [0204] In some embodiments, a minimum of 95% of the beads are perfectly spherical. | [0205] In one embodiment, the amine-functionalised beads are amino C2 methacrylate beads, wherein the particle size range is 150 to 300 micron, the pore diameter is 600 to 1200 A, andthe total moisture is 62 to 72%. The functional group is amino (short spacer). The beads are typically stable at pH 3 to pH 10, and suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0206] In one embodiment, the amine-functionalised beads are amino C2 methacrylate beads, wherein the particle size range is 150 to 300 micron, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is amino (short spacer). The beads are typically stable at pH 3 to pH 10, and are suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0207] In one embodiment, the amine-functionalised beads are amino C6 methacrylate beads, wherein the particle size range is 150 to 300 micron, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is amino (short spacer). The spherical beads are stable at pH 3 to pH 10, and are suitable for storage at 2 to 20 oC. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0208] Adsorbent resins | [0209] In some embodiments, the bead is an adsorbent resin bead. Adsorbent beads immobilise the protein or peptide by adsorption. Proteins or polypeptides with hydrophobic properties can be efficiently immobilised onto adsorbent beads. Adsorbent resins are water-insoluble carriers that allow physical adsorption of an enzyme onto its surface. | [0210] In some embodiments, the bead is a polystyrenic, non-functionalised resin bead. In some embodiments, the bead is an octadecyl methacrylate bead. In some embodiments, the bead is a polymethacrylic/divinylbenzene bead. In some embodiments, the bead is a polymethacrylic/divinylbenzene macroporous bead. In some embodiments, the polymer structure is polymethacrylic crosslinked with divinylbenzene. | [0211] Adsorbent beads can be used with the invention because they immobilise proteins or polypeptides with high mechanical stability. | [0212] In some embodiments, the particle size range is 300 to 1200 micron. Optionally, the particle size range is 300 to 710 micron, or 350 to 1200 micron. | [0213] In some embodiments, the pore diameter is 220 to 1200 A. Optionally, the pore diameter is 900 to 1100 A, 400 to 650 A, 220 to 340 A, or 350 to 1200 A. | [0214] In some embodiments, the total moisture is 57 to 78%. Optionally, the total moisture is 67 to 78%, 58 to 63%, 57 to 68%, or 60-66%. | [0215] In some embodiments, the typical pore diameter by nitrogen adsorption is 300 A. In some embodiments, the typical pore volume by nitrogen adsorption is 1.2 mL/g. In some embodiments, the typical surface area by nitrogen adsorption is 490 m2/g.In some embodiments, the specific gravity is 1.1. | [0216] In some embodiments, a minimum of 95% of the beads are perfectly spherical. | [0217] In some embodiments, the adsorbent bead has a functional group. Optionally the adsorbent bead has an amino functional group. Optionally, the functional group is non-ionic. | [0218] In one embodiment, the adsorbent bead is a polystyrenic, non-functionalised resin bead, wherein the particle size range is 300 to 710 micron, the pore diameter is 900 to 1100 A, and the total moisture is 67 to 78%. The spherical beads are stable at pH 1 to pH 14, and are suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0219] In one embodiment, the adsorbent bead is an octadecyl methacrylate bead, wherein the particle size range is 300 to 710 micron, the pore diameter is 400 to 650 A, and the total moisture is 58 to 63%. The functional group is amino (short spacer). The spherical beads are stable at pH 2 to pH 10, and are suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0220] In one embodiment, the adsorbent bead is a polymethacrylic/divinylbenzene, nonfunctionalised resin bead, wherein the particle size range is 300 to 710 micron, the pore diameter is 220 to 340 A, and the total moisture is 57 to 68%. The beads are typically stable at pH 1 to pH 14, and are suitable for storage at 2 to 20°C. Optionally, a minimum of 95% of the beads are perfectly spherical. | [0221] In one embodiment, the adsorbent bead is a polymethacrylic/divinylbenzene macroporous, adsorbent resin bead in a non-ionic form, wherein the particle size range is 350 to 1200 micron, the typical pore diameter by nitrogen adsorption is 300 A, the typical pore volume by nitrogen adsorption is 1.2 mL/g, the typical surface area by nitrogen adsorption is 490 m2/g, the specific gravity is 1.1 , and the moisture retention is 60-66%. The functional group is non-ionic and the polymer structure is polymethacrylic crosslinked with divinylbenzene. The spherical beads are stable at pH 0 to pH 14, and the temperature limit is 100°C. | [0222] Ion exchange resins | [0223] In some embodiments, the bead is an ion-exchange resin. In some embodiments, the ionexchange resin is a cation exchange resin or an anion exchange resin. | [0224] In some embodiments, the ion-exchange resin comprises polystyrene crosslinked with divinylbenzene.Examples of epoxy, amine and adsorbent beads that are commercially available from Purolite Ltd. (Llantrisant, Wales, UK) are provided below along with their catalogue numbers. | [0225] Epoxy resins: | [0226] ECR8204F | [0227] • Epoxy-functionalised resin | [0228] • Purolite “perfect bead”: min. 95%. | [0229] • Epoxy methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 300 to 600 A, and the total moisture is 50-65%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage from 2 to 8°C. | [0230] ECR8285 | [0231] • Epoxy-functionalised resin | [0232] • Purolite “perfect bead”: min. 85%. | [0233] • Epoxy/butyl methacrylate beads, wherein the particle size range is 250 to 1000 pm, the pore diameter is 450 to 650 A, and the total moisture is 70 to 80%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage at 2 to 8°C. | [0234] ECR8215F | [0235] • Epoxy-functionalised resin | [0236] • Purolite “perfect bead”: min. 95%. | [0237] • Epoxy methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is epoxy. The spherical beads are stable at pH 5 to pH 9, and are suitable for storage at 2 to 8°C. | [0238] Adsorbent resins: | [0239] ECR1090M | [0240] • Adsorbent resin• Purolite “perfect bead”: min. 95%. | [0241] • Functional group: none. | [0242] • Polystyrenic, non-functionalised resin beads, wherein the particle size range is 300 to 710 pm, the pore diameter is 900 to 1100 A, and the total moisture is 67 to 78%. The spherical beads are stable at pH 1 to pH 14, and are suitable for storage at 2 to 20°C. | [0243] ECR8806M | [0244] • Adsorbent resin | [0245] • Purolite “perfect bead”: min. 95%. | [0246] • Octadecyl methacrylate beads, wherein the particle size range is 300 to 710 pm, the pore diameter is 400 to 650 A, and the total moisture is 58 to 63%. The functional group is amino (short spacer). The spherical beads are stable at pH 2 to pH 10, and are suitable for storage at 2 to 20°C. | [0247] ECR1030M | [0248] • Adsorbent resin | [0249] • Purolite “perfect bead”: min. 95%. | [0250] • Functional group: none. | [0251] • Polymethacrylic/divinylbenzene, non-functionalised resin beads, wherein the particle size range is 300 to 710 pm, the pore diameter is 220 to 340 A, and the total moisture is 57 to 68%. The spherical beads are stable at pH 1 to pH 14, and are suitable for storage at 2 to 20°C. | [0252] PAD610 | [0253] • Adsorbent resin | [0254] • Polymethacrylic/divinylbenzene macroporous, adsorbent resin beads in a non-ionic form, wherein the particle size range is 350 to 1200 pm, the typical pore diameter by nitrogen adsorption is 300 A, the typical pore volume by nitrogen adsorption is 1.2 mL/g, the typical surface area by nitrogen adsorption is 490 m2/g, the specific gravity is 1.1 , and the moisture retention is 60-66%. The functional group is non-ionic and thepolymer structure is polymethacrylic crosslinked with divinylbenzene. The spherical beads are stable at pH 0 to pH 14, and the temperature limit is 100°C. | [0255] Amine resins: | [0256] ECR8309F | [0257] • Amine-functionalised resin | [0258] • Purolite “perfect bead”: min. 95%. | [0259] • Amino C2 methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 600 to 1200 A, and the total moisture is 62 to 72%. The functional group is amino (short spacer). The spherical beads are stable at pH 3 to pH 10, and suitable for storage at 2 to 20°C. | [0260] ECR8315F | [0261] • Amine-functionalised resin | [0262] • Purolite “perfect bead”: min. 95%. | [0263] • Amino C2 methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is amino (short spacer). The spherical beads are stable at pH 3 to pH 10, and are suitable for storage at 2 to 20°C. | [0264] ECR8415F | [0265] • Amine-functionalised resin | [0266] • Purolite “perfect bead”: min. 95%. | [0267] • Amino C6 methacrylate beads, wherein the particle size range is 150 to 300 pm, the pore diameter is 1200 to 1800 A, and the total moisture is 70 to 80%. The functional group is amino (short spacer). The spherical beads are stable at pH 3 to pH 10, and are suitable for storage at 2 to 20°C.Rocks | [0268] A rock is a solid mass of geological material. In the present invention, the rock may be a source of metal cations. | [0269] Cations | [0270] Metal cations used in the method of the present invention include one or more of Mg2+, Ca2+. | [0271] Rock composition | [0272] According to the present invention, one or more rock types may be applied to soil, as is known in the technique of “enhanced weathering”. | [0273] In some embodiments, the rock comprises silica. In some embodiments, the rock comprises or consists of basalt. In some embodiments the rock comprises or consists of olivine. | [0274] In some embodiments, the rock comprises carbonates. In some embodiments, the rock comprises limestone. | [0275] Rock preparation | [0276] Prior to application to the soil, rocks that may be used in the method of the present invention may optionally be reduced in size, compared to an initial size, for example to increase rate of enhanced weathering. For example, a boulder may be reduced to a sand, or a pebble may be reduced to a powder or other particulate material typically less than e.g. 5mm or 1 mm diameter. In some embodiments, the rock is reduced in size by any one or combination of crushing, grinding, sieving, milling, pulverisation, and/or ball milling. | [0277] In some embodiments, the rock is particulate and has an average particle size of at least 1 micrometre. In some embodiments, the rock is particulate and has an average particle size of 5 millimetres or less. In some embodiments, the rock is particulate and has an average particle size of 4 millimetres or less. In some embodiments, the rock is particulate and has an average particle size of 1000 micrometres or less. In some embodiments, the rock is particulate and has an average particle size of 750 micrometres or less. In some embodiments, the rock is particulate and has an average particle size of 500 micrometres or less. In some embodiments, the rock is particulate and has an average particle size of 300 micrometres or less. In some embodiments, the rock is particulate and has an average particle size 1 micrometre to 300 micrometres. In some embodiments, the rock is particulate and has an average particle size of 400 micrometres or more. In some embodiments, the rock is particulate and has an average particle size of 500 micrometres or more. In some embodiments, the rock is particulate and has an average particle size of about 500 micrometres to about 4 millimetres. In some embodiments, the rock is particulate and hasan average particle size of about 500 micrometres to about 2000 micrometres, or about 500 micrometres to about 1500 micrometres, or about 500 micrometres to about 1000 micrometres, or about 500 micrometres to about 750 micrometres. Any appropriate method for determining particle size may be applied, as known in the art. One simple but effective method for sizing rock particles is sieve analysis, as is well known in the art. There are 2 types of sieve analysis that can be carried out: wet sieving and dry sieving. Wet sieving is suitable for particle sizes from 20pm up to 3mm while dry sieving is suitable for particles from 30pm up to 125mm. | [0278] In some embodiments, the rock is particulate and has an average particle size of at least about 500 micrometres to about 10 millimetres. In some embodiments, the rock is particulate and has an average particle size of at least about 500 micrometres to about 5 millimetres. In some embodiments, the rock is particulate and has an average particle size of at least about 0.5 millimetres to about 4 millimetres. In some embodiments, the rock is particulate and has an average particle size of at least about 500 micrometres to about 2 millimetres. In some embodiments, the rock is particulate and has an average particle size of at least about 500 micrometres to about 1 millimetre. | [0279] In some embodiments, the rock is reduced in size to a dust. In some embodiments, the rock is reduced in size to a powder. In some embodiments, the rock is reduced in size to particulates. In some embodiments, the rock is reduced in size to sand. | [0280] In some embodiments, the rock is applied to the soil as a dust or sand. In some embodiments, the rock is applied to the soil as a powder. In some embodiments, the rock is applied to the soil as particulate matter. | [0281] Application | [0282] Carbonic anhydrase and optionally rock are applied to soil in one aspect of a method of the present invention. | [0283] In some embodiments, the Carbonic Anhydrase and rock are applied to the soil simultaneously. Optionally, the Carbonic Anhydrase and rock are pre-formulated together prior to application, or are applied simultaneously from two or more different sources. Optionally, the Carbonic Anhydrase and rock are mixed together prior to application. | [0284] In some embodiments, the Carbonic Anhydrase and rock are applied to the soil contemporaneously. | [0285] In some embodiments, the Carbonic Anhydrase and rock are applied to the soil at different times. In some embodiments, the Carbonic Anhydrase and/or rock are applied to the soil two or more times, optionally two or more times in a day, a week, a month, a season, or a year.Frequency | [0286] In some embodiments, the Carbonic Anhydrase and/or rock is applied to the soil once a year. In some embodiments, the Carbonic Anhydrase and/or rock is applied to the soil twice or more a year. In some embodiments, the Carbonic Anhydrase and/or rock is applied to soil over one or more years. | [0287] In some embodiments, the Carbonic Anhydrase and/or rock is applied to the soil prior to planting crops. | [0288] Method | [0289] The Carbonic Anhydrase and/or the rock can be applied to the soil in different ways. | [0290] In some embodiments, the Carbonic Anhydrase and/or rock is sprayed onto soil. In some embodiments, the Carbonic Anhydrase and/or rock is spread onto soil. | [0291] In some embodiments, spreading can occur by hand. In some embodiments, spreading can occur by machine. In some embodiments, the spraying can occur by machine. In some embodiments, the Carbonic Anhydrase and/or rock can be dug into the soil, optionally by mixing and/or churning. | [0292] Typically, application will be done using machinery over one or more acres. In some embodiments, application will be done using machinery over ten or more acres, fifty or more aces, seventy or more acres, one hundred or more acres, two hundred or more acres, five hundred or more acres, one thousand or more acres, five thousand or more acres, ten thousand or more acres, twenty thousand or more acres. In some embodiments, application will be done using machinery over five or more hectares, ten or more hectares, fifty or more hectares, seventy or more hectares, one hundred or more hectares, two hundred or more hectares, five hundred or more hectares, one thousand or more hectares, five thousand or more hectares, ten thousand or more hectares. | [0293] Soil, Earth, Ground, Ocean | [0294] In some embodiments of the present invention, Carbonic Anhydrase and optionally rock are applied to soil. This attenuates, prevents, or reverses soil acidification. | [0295] In some embodiments, Carbonic Anhydrase and rock are applied to ground. The ground may or may not comprise soil. For example the ground may be scrubland or rocky ground. The ground may have plant cover, for examples grasses or trees. | [0296] In some embodiments, there is not substantial plant cover over the soil. Typically, the soil comprises or consists of bare soil. The rock and Carbonic Anhydrase can therefore directly contact the bare soil.Soil organic carbon (SOC) is the overall soil carbon content of a soil and may also be generally referred to as total organic carbon (TOC) (the terms may be used interchangeably), and this refers only to the carbon component of the organic matter in the soil. However, fluctuations in soil organic carbon may not necessarily correlate to the same fluctuations in stable soil carbon. Indeed, soils subjected to the treatments and methods may demonstrate minimal increases in TOC, but the percentage of said TOC that is captured in a stable form in the soil or in the fungi proliferating in the soil (i.e., complex polysaccharides, melanin, chitin, lignin, suberin and carotenoid compounds) may increase. The skilled addressee would also understand that changes in TOC and stable carbon in soil as a result of the treatments and methods of the present may take weeks, months or years, and therefore appropriate measurement timeframes must be applied. In one embodiment, the increase in soil organic carbon in a soil comprises an increase in stable carbon in the soil. | [0297] The soil carbon may be measured by methods including, but not limited to, dry combustion or elemental tests that may be analysed using, for example, the LECO analysis method, and loss on ignition (LOI) tests that may be analysed using the Walkley-Black method (see, for example, Walkley A, and Black IA (1934) An examination of the Degtjareff method for determining soil organic matter, and a proposed modification of the chromic acid titration method. Soil Science 37 , 29-38). To assess the prevalence of different types of carbon on the TOC (i.e. to measure the stable, or "recalcitrant" organic carbon), methods may be employed to fractionate to TOC by, for example, measuring soil respiration or the bulk density of the soil. | [0298] In some embodiments, the applying step comprises spraying the Carbonic Anhydrase onto the soil or ground. The Carbonic Anhydrase may be present in a slurry when sprayed, for example a fertilising slurry of the sort often used in agriculture. The slurry may comprise rock as described extensively herein. The Carbonic Anydrase, optionally in the form of a slurry, may be sprayed onto the soil or ground using agricultural equipment for example a spray bar or broadcast spreader. | [0299] While the disclosure focuses on solid ground, it can also be applied to large bodies of water such as in an ocean, sea or lake. All technologies of enhanced weathering where finely ground rock is deposited on or in an extensive area, e.g. farm, forest, ocean, lake or sea are contemplated within the scope of the invention. | [0300] Land | [0301] In some embodiments, the soil or ground is within agricultural land. In some embodiments, the soil or ground is within arable land. In some embodiments, the soil or ground is within pasture land.In some embodiments, the soil or ground is within pasture land. In some embodiments, the soil or ground is within waste land. In some embodiments, the soil or ground is within brownfield land. In some embodiments, the soil is within industrial land. | [0302] Depth | [0303] The present invention can advantageously retain Carbonic Anhydrase within a desired range of soil depth. | [0304] Typically, the Carbonic Anhydrase is retained in the top soil. Methods of measuring the depth of top soil are well known in the art. Typically, the depth of the top soil is measured downwards from the surface of the soil. | [0305] In some embodiments, the top soil extends 2 metres or less from the soil surface, and the Carbonic Anhydrase is retained in that region. In some embodiments, the top soil extends 1 metre or less from the soil surface. In some embodiments, the top soil extends 50 centimetres or less from the soil surface. In some embodiments, the top soil extends 30 centimetres or less from the soil surface. In some embodiments, the top soil extends 25 centimetres or less from the soil surface. In some embodiments, the top soil extends 20 centimetres or less from the soil surface. In some embodiments, the top soil extends 15 centimetres or less from the soil surface. In some embodiments, the top soil extends 10 centimetres or less from the soil surface. In some embodiments, the top soil extends 5 centimetres or less from the soil surface.| [0306] In some embodiments, the Carbonic Anhydrase is retained substantially on the surface of the top soil. For example, in some embodiments the Carbonic Anhydrase is retained in the top 5 cm of the soil, or the top 1 cm of the soil. In these embodiments, Carbonic Anhydrase remains exposed directly to the surface air and is not buried in the soil. | [0307] Increasing crop yield | [0308] In the present invention, Carbonic Anhydrase and optionally rock are applied to soil. The Carbonic Anhydrase may be applied to the soil in the form of being immobilised to a seed that is sown into the soil. The Carbonic Anhydrase may be applied to the soil in the form of being immobilised to a plant that is planted into the soil, optionally wherein the Carbonic Anhydrase is immobilised to the plant root. The seed coat and/or plant root may remain in the soil after the plant or a part of the plant is harvested, thereby also retaining the Carbonic Anhydrase in the soil. This attenuates, prevents, or reverses soil acidification, which can increase land productivity. In some embodiments of the invention, land productivity is increased after application of Carbonic Anhydrase and rock to soil. | [0309] For example, crop yields in the subsequent year or years can increase. In some embodiments, the crop yield obtained from land treated by application of Carbonic Anhydrase and optionallyrock to soil is increased by 5% or more compared to the previous crop yield from the same land. In some embodiments, crop yields are increased by 10% or more, 15% or more, 20% or more, 25% or more. | [0310] In other embodiments, the crop yield obtained from land treated by application of Carbonic Anhydrase and optionally rock to soil is increased by 5% or more compared to untreated land. In some embodiments, crop yields are increased by 10% or more, 15% or more, 20% or more, 25% or more. | [0311] The time taken to obtain increased crop yield can be over one or more years. In some embodiments, the crop yield is increased in the subsequent year to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased two years subsequent to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased three years subsequent to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased four years subsequent to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased five years subsequent to the first application of Carbonic Anhydrase and rock to soil. In some embodiments, the crop yield is increased six years subsequent to the first application of Carbonic Anhydrase and rock to soil. | [0312] In some embodiments, the land retains higher productivity after application of Carbonic Anhydrase and rock to soil compared to untreated soil. | [0313] In some embodiments, the crop yields are higher in land treated by application of Carbonic Anhydrase and rock to soil compared to crop yields obtained from land treated by application of rock to soil alone. In some embodiments, the crop yields are higher in land treated by application of Carbonic Anhydrase and rock to soil compared to crop yields obtained from land not treated by application of carbonic anhydrase. | [0314] EMBODIMENTS | [0315] The disclosure further provides the following numbered embodiments as provided below, which are intended to define further the disclosed technologies but not intended to limit the scope of the invention. | [0316] 1. A method of sequestering atmospheric carbon, comprising the step of applying Carbonic Anhydrase and rock to soil. | [0317] 2. The method of embodiment 1 , wherein the Carbonic Anhydrase is immobilised to a solid support. | [0318] 3. The method of embodiment 2, wherein the solid support comprises or consists of:plant matter, optionally wherein the plant matter comprises or consists of corn husks and/or cellulose; and/or animal matter; and/or fibrous materials; and/or a bead; optionally wherein the solid support comprises or consists of waste material. | [0319] 4. The method of embodiment 2 or 3, wherein the solid support has a procurement cost of $20 or less per kg, $10 or less per kg, $5 or less per kg, $1 or less per kg, or $0.5 or less per kg. | [0320] 5. The method of embodiment 1 , wherein the Carbonic Anhydrase is immobilised to the rock, optionally directly to the rock, optionally by covalent bond or by non-covalent means such as physical adsorption. | [0321] 6. The method of any preceding embodiment, wherein the Carbonic Anhydrase has a structural modification to the enzyme which is intended to increase retention at a specified depth and/or location in the soil. | [0322] 7. The method of any preceding embodiment, wherein the Carbonic Anhydrase is retained in top soil; optionally wherein the top soil extends 1 metre or less from the soil surface, optionally 50 centimetres or less, 30 centimetres or less, 25 centimetres or less, 20 centimetres or less, 15 centimetres or less, or 10 centimetres or less. | [0323] 8. The method of any preceding embodiment, wherein the Carbonic Anhydrase is substantially retained at or around the roots of a plant, optionally in contact with one or more roots. | [0324] 9. The method of any preceding embodiment, wherein the soil is within: agricultural land, optionally wherein the agricultural land is arable land or pasture land; waste land; brownfield land; or industrial land. | [0325] 10. The method of any preceding embodiment, wherein the Carbonic Anhydrase and rock are applied to the soil simultaneously, contemporaneously or at different times.11. The method of any preceding embodiment, wherein the rock is a source of metal ions; optionally wherein the metal ions are cations, optionally wherein the cations are any of Mg+2 or Ca+2. | [0326] 12. The method of any preceding embodiment, wherein the rock comprises silica, optionally wherein the rock comprising silica is basalt or olivine. | [0327] 13. The method of any preceding embodiment, wherein the method comprises the step of reducing the rock in size before application to the soil, optionally wherein the rock is reduced in size by crushing, grinding, sieving, milling, pulverisation, and/or ball milling. | [0328] 14. The method of any preceding embodiment, wherein the rock is applied to the soil as a dust, powder, or particulate. | [0329] 15. The method of any preceding embodiment, wherein the Carbonic Anhydrase comprises an animal carbonic anhydrase, a plant carbonic anhydrase, and/or a bacterial carbonic anhydrase; optionally wherein the animal Carbonic Anhydrase comprises bovine erythrocyte carbonic anhydrase. | [0330] 16. The method of any preceding embodiment, wherein the Carbonic Anhydrase comprises an alpha, beta, delta, gamma, or zeta carbonic anhydrase. | [0331] 17. The method of any preceding embodiment, wherein the atmospheric carbon is sequestered as a carbonate, optionally as a magnesium carbonate or a calcium carbonate. | [0332] 18. A sequestered carbon obtained or obtainable by the method of any of embodiments 1 - 17. | [0333] 19. A mixture comprising Carbonic Anhydrase and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0334] 20. A mixture comprising Carbonic Anhydrase and rock, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0335] 21. A mixture comprising carbonic anhydrase, rock and soil, optionally wherein the Carbonic Anhydrase is immobilised to a solid support. | [0336] 22. Use of a mixture according to any of embodiments 19 - 21 to sequester atmospheric carbon. | [0337] 23. A mixture according to any of embodiments 19 - 21 , for use in sequestering atmospheric carbon.24. A method of spraying an enzyme slurry or otherwise coating rock in a way that is compatible with agricultural equipment, e.g. a spray bar on a piece of broadcaster equipment. | [0338] 25. Carbonic anhydrase enzyme within a cell and bound to rock, such as via adsorption to rock particles of a cell that expresses Carbonic Anhydrase. | [0339] EXAMPLES | [0340] Summary: Carbon capture product to accelerate enhanced weathering. | [0341] Test suitability of commercially-available Carbonic Anhydrase (CA) enzyme for accelerated enhanced weathering using agriculturally acceptable solid carriers. Test activity and stability of the free enzyme under industrially relevant conditions (e.g. Temperature 4-20°C, ambient CO2, neutral and basic pH). Using commercial Carbonic Anhydrase enzyme, perform industrially relevant bead screens (e.g. basalt, vermiculite, perlite) for stability and activity. | [0342] Background. | [0343] - **Basalt.** In geology basalt reacts with CO2 from rain water to produce magnesium and calcium salts, such as, bicarbonate to store this mineral in the ground for millions of years. Basalt is mainly composed of SiO2 (45-52%), with CaO (5-10%), MgO (9.7%) and Na2<D (5.3%) plus many other metal oxides such as AI2O3 (13.1%) and Fe2Os (13.8%). [Basalt is negatively charged.] | [0344] - **Advanced weathering.** Accelerate this natural process by spreading raw and processed basalt on fields to capture and store CO2. | [0345] - **Carbonic anhydrase.** This is found in nature and converts CO2 and H2O into carbonic acid and protons, we want to utilise this enzyme to accelerate the advanced weathering phenomena by coating the enzymes directly on basalt rocks. It [converts 1 ,000,000 CO2 molecules per second]. This enzyme has been shown to bind to silica gel previously - see https://pubmed.ncbi.nlm.nih.gov/18584683/. | [0346] - **CO2 produced per year.** Across the world 93,000,000 barrels of oil are used per day (1 barrel = 200 L). CO2 emissions equate to 36.8 billion tonnes per year. We need to remove 1 billon tonnes per year to help slow down global warming.- **Alternative rocks.** Other rock types or minerals can also exhibit favourable properties for this application - see (https://en wikipedia.org/wiki/List of rock types). However most researchers are focused towards basalt. | [0347] - **Bead screen.** Initially we planned to perform a bead screen using a variety of agricultural beads, including basalt, vermiculite and perlite, plus and minus coating agents to improve stability. However looking into the feasibility of the project in more detail we realised it only makes sense to coat the enzyme directly onto basalt for the current application. Veolia have supplied two types of basalt, *raw* and *processed*. The latter is smaller and has a higher water content by around 30-40% v/w. | [0348] Key findings | [0349] CA from a commercial source is highly concentrated and active > Sigma Carbonic Anhydrase extracted from cows > bovine serum. | [0350] CA is able to turn over 4-nitrophenyl acetate or CO2. | [0351] CA is able to accelerate CO2 conversion using either NaCI, MgCI2, CaCI2 or basalt. | [0352] CA is able to bind and remain stable for up to 1 month at RT to either basalt, silica gel with or without fragmentation. | [0353] CA immobilised on basalt is stable and remains active over 4 uses. | [0354] CA from a commercial source loads 10 pL of enzyme onto 1 g of raw or processed basalt in 30 mins at RT in tap water. | [0355] Carbonic Anhydrase should be diluted down to 50L in tap water and then sprayed onto basalt directly on the field. | [0356] Carbonic Anhydrase can get washed off basalt rocks in soil so careful attention must be paid to how it interacts with soil. | [0357] Carbonic Anhydrase immobilised on silica gel is able to turn over CO2 and react with “sea water” in flow leading to a sea-based product. | [0358] Example 1 : Exemplary immobilisation soil test protocol | [0359] - Take 50L of 1x PBS buffer in a >50L container. Add the buffer reagent to the >50L container.| [0360] - Add 250g of Silica Gel | [0361] - Add 6g of enzyme | [0362] - Agitate/mix with a stirrer for 4hrs at room temp (25-30°C)- Apply directly to the soil as a wet solution. obtained from residual blood from meat| [0363] Bovine blood typically contains 7-15% w/v of CA. In this example, CA was obtained from residual blood from grocery store steaks, from Amazon and Sainsbury’s. In its unpasteurised form, milk contains CA. However, the pasteurisation process was expected to denature the majority, if not all, of the Carbonic Anhydrase. Therefore, pasteurised milk was used as a negative control in these experiments. | [0364] Method: 20 pL of blood solution was extracted from steaks obtained from Amazon and Sainsburys and placed into 180 pL water, then performed a 1 in 2 serial dilution. 10 pL of this liquid was used in a 4-nitrophenol acetate (4-NPA) assay. The 4-NPA assay involves the hydrolysis of 4-NPA by CA, and is described, for example in Shank et al. (2006) Chemical Biology & Drug Design 68(2)113-119. Specifically, 4-NPA, which is colourless, is hydrolysed to 4-nitrophenol (4-NP), which is yellow, and acetate. This colour change provides a spectrophotometric optical density readout. | [0365] Specifically, the 10 pL of and placed into 50 pL of 4-NPA mastermix in a 384-well plate. The absorbance was scanned at 400 and 500 nm. | [0366] Outcome: CA from both Amazon and Sainsbury’s was able to convert 4-NPA to 4-NP. As expected, pasteurised milk contained no active CA. Figure 1A shows outcome of the 4-NPA assay when serial dilutions of the blood solution obtained from the Amazon steak were used. Figure 1 B shows the product titre obtained from CA obtained from Amazon steak, Sainsbury’s steak, or pasteurised milk. | [0367] This example demonstrates that active CA can be obtained from an animal or part thereof, for example from the blood of the animal. | [0368] Example 3. CA obtained from animal blood has comparable activity to commercial CA. | [0369] This example shows that commercially-available CA, bovine serum, and blood from steak and minced beef show 4-NPA activity. | [0370] The 4-NPA assay described in Example 2 was repeated. Specifically, 1 mL of each CA source, underwent a 1 in 2 serial dilution, into a 96 deep well plate. Next, 10 pL of solution was added to 50 pL of 4-NPA mastermix in a 384-well plate. The profiles were plotted and the slopes generated. Figure 2A is a plot of activity slopes of the stated CA source assayed. Figure 2Bshows the activity kinetic plot of the buffer only, as negative control. Figure 2C shows activity kinetic plot for commercial CA with varying enzyme amount. Figure 2D shows activity kinetic plot for CA obtained from blood sample obtained from steak. Note, steak had a high background due to particle scattering, therefore the 5 pL plot was used to compare side-by- side. | [0371] Next, the thermal melting profile of the free enzymes was assessed. | [0372] Method: Commercial CA was diluted 1 in 5 into tap water, and steak blood was diluted 1 in 2 into tap water. The enzyme solution was transferred to 100 pL to 8x PCR tubes and heated at the stated temperature for 10 mins. Next, 10 pL of solution was added to 50 pL of 4-NPA mastermix in a 384-well plate and the 4-NPA assay as described in Example 2 was performed. The normalised profiles were plotted and the slopes generated. | [0373] Results: Figure 3 shows steak CA enzymes denature between 50 and 60 degrees, whilst the commercially-available CA did not unfold at all. | [0374] Example 4. Immobilising enzyme to different solid supports. | [0375] This example demonstrates that CA from various sources is able to bind and turn over product on sand, silica gel, chalk and dolomite. | [0376] Methods: 200 mg of the stated material was added to 100 pL of the stated crude enzyme. The enzyme was allowed to immobilise for 30 mins by shaking at 1250 r.p.m. at room temperature. The supports were washed by performing 5x wash-centrifugation cycles (except for the free enzyme controls which were not washed). Next, a 4-NPA activity assay was performed by adding 1 mL 4-NPA mastermix and shaking at 1250 r.p.m. for 30 minutes, isolating 50 pL of supernatant and transferring to a 384-well plate. The amount of product formed was plotted.| [0377] Results: Figure 4 shows CA from both sources was able to bind and turn over 4-NPA on sand, silica gel, chalk and dolomite. The commercial enzyme was added in about 5x excess, whilst the blood ratio was more efficient with almost quantitative loading. | [0378] Example 5. Carbonate formation. | [0379] This example demonstrates that CA obtained from bovine blood is able to capture and convert CO2 into sodium carbonate and or calcium carbonate using sea water.Method: 1 g of silica gel with or without 200 pL of Amazon CA was weighed out and placed in a 50 mL falcon tube and left to immobilise for 30 minutes. 10 mL sea water containing 1 M tris base at pH 10.5 was then added to control the pH shift. 1 mL of this mix was extracted and 100 pL of concentrated HCI was added. The falcon tube was heated to 50 degrees and 3x cardice (i.e., dry ice) cubes were added. After 10 minutes 1 mL was extracted and 100 pL of concentrated HCI was added. | [0380] Results: Figure 5 shows extensive bubble formation for CA obtained from bovine blood after the addition of cardice, indicating efficient CO2 capture and conversion to sodium carbonate or calcium carbonate. | [0381] Example 6 | [0382] In 6x 50 mL falcon tubes, either 0, 1 , or 10 mL of crude CA from a commercial source was added to 0.5 g of raw “R” or processed “P” basalt, supplemented with 0.1 M NaPi pH 7.0 (25 mL). All volumes were equal. Next, the falcon tubes were placed in a water bath set to 50 degrees, after 5 minutes single blocks of cardice were added and the colour change monitored. After 10 minutes, 50 pL was extracted and scanned the absorbance in a 384-well plate using the plate reader. | [0383] Pictures and absorbance profiles did not show the corresponding change in acid, potentially the basalt interacts with the indicator to corrupt the readout. Also, no apparent change in basalt mass was observed. | [0384] Figure 6 shows that bubbles formed when either raw “R” or processed “P” basalt was provided to the mix. | [0385] Example 7 | [0386] This example demonstrates that CA isolated from blood can be immobilised on CaCO3 and improve its thermal stability. | [0387] Method: 0.25mg of CaCO3 -/+ 200 uL of steak blood CA was added to a 1 .5 mL vial and left to immobilise for 30 minutes. The immobilised CA was then washed in water by performing 5x wash-centrifugation cycles. Next, the immobilised CA was moved into 100 uL PCR tubes and heated to the stated temperature for 10 minutes. Next, 100 uL of 4-NPA mastermix was added in a 384-well plate and mixed for 10 mins shaking at 1250 r.p.m., then extracted 50 uL supernatant. The absorbance was scanned. The normalised profiles were plotted and the slopes generated.Figure 7 shows CA can be stabilised on CaCO3 (chalk) and turn over 4-NPA product up to 60°C. | [0388] Overview of Examples 8 to 18 | [0389] The following examples show that the CO2 sequestration is effective for different sources of basalt. The use of a calcimeter provides a reproducible method for verification. | [0390] Example 8 | [0391] This example explains how measurements using a Calcimeter in subsequent examples were conducted. | [0392] Method: This analysis was performed using FOGL Bench-top Soil Calcimeter™ from bd Inventions. 5 g of sample was weighed into the sample container. 6 mL of 50% HCI (concentrated HCI diluted 1 :1 v/v using double distilled water) was added into the HCI container of the instrument. The sample weight was registered as 5 g and the measurement was initiated by pressing ‘start’ on the software. The lid was closed and all connections were ensured to be secure and airtight. The sample was mixed for 10 s and rested. The resulting change in partial pressure due to CO2 was measured by the instrument and reported as the %CO2 equivalents of CaCO3. | [0393] Example 9 | [0394] This example demonstrates free enzyme activity in water. | [0395] Method: 0.25 uL of a CA obtained commercially, 10 mL of water and 0.5 mL of 5 M CaCI2 were mixed. A negative control reaction was also set up, where water was used instead of enzyme. Each reaction was incubated at 60°C for 5 min in the water bath. Next, one block of equal sized dry ice was added into each tube and the experimentalist waited until the bubbling had stopped to close the tubes and incubate the tubes at 30°C for 5 min in a shaker, for the tubes were centrifuged for 5 min at 4,500 x rpm. The supernatant was decanted and the pellet was resuspended in 1 mL of ddH2O. The %CO2 for the 1 g sample was then measured using the Calcimeter. | [0396] Table 1 Variation of %CO2 equivalents for free enzyme reaction.No pellet had formed after the reaction, most likely because the dry ice added was not sufficient for the reaction to proceed within the limited time. | [0397] Example 10 | [0398] This example demonstrates the effect of buffer on the free enzyme reaction. | [0399] Method: 2 mL of a CA obtained commercially or, for negative control, buffer only, 10 mL of 1.5 M Tris-HCI pH 9.1 or 0.5 M Tris-HCI pH 8.5 (the experiment was performed using each type of buffer) and 0.5 mL of 5 M CaCI2 were mixed in a 50 mL Falcon tube. The tubes were then incubated in a water bath set to 60°C for 15 min in a fume hood. A small piece of dry ice was placed into each 50 mL Falcon tube. The reaction was allowed to proceed until the dry ice fumes stopped being released from the tubes. The tubes were incubate in the shaking incubator for 5 min (set to 37°C). The tubes were then centrifuged for 1 min at 4,300 x ref. The supernatant was decanted from the tubes. The pellets were resuspended in 1 mL of ddH2O. The calcimeter was set to measure 1 g of material; 1 mL of resuspended pellet from 2h was pipetted into the Calcimeter's Duran bottle and determine the carbonate content using the Calcimeter. | [0400] The outcome of the experiment is shown in Figure 8, where it was found that 1.5M Tris HCI buffer pH 9.1 is better for free carbonic anhydrase reaction. | [0401] Example 11 | [0402] This example demonstrates the effect of CaCI2 on free enzyme activity. | [0403] Method: Three tubes containing 0.25 uL of a commercially obtained CA and 10 mL of 1.5 M Tris pH 9.1 were set up. Either 0.1 mL of 5 M CaCI2 (Tube 1), 0.5 mL of 5 M CaCI2 (Tube 2) or 1 mL of 5 M CaCI2 (Tube 3) were added to each tube, which were then incubated at 60°C for 5 min in a water bath in a fume hood. One block of equal sized dry ice was added into each tube and the experimentalist waited until the bubbling had stopped before closing the tubes and incubating the tubes at 30°C for 5 min in the shaker. The tubes were then centrifuged for 5 min at 4,500 x rpm. The supernatant was decanted and the pellet was resuspended in 1 mL of ddH2O. The % CO2 for the 1 g sample was measured using the Calcimeter. | [0404] Table 2 Variation of %CO2 equivalents with CaCI2 concentration for free enzyme reaction.It was found 0.5 M CaCI2 was the optimum concentration to achieve the highest CO2 sequestration using free enzyme. | [0405] Example 12 | [0406] This example compares of carbonic anhydrase performance on Silica gel or basalt in buffered reaction. | [0407] Method: 1 mL of CA obtained commercially or ddH2O were mixed with 10 g of either Remin basalt (Rb), Duntilland basalt (Db) or 2.5 g of Silica gel (SG) in a 50 mL Falcon tube. 10 mL of 1.5 M Tris pH 9.1 buffer was added to each tube. The tubes were incubated on the rotor for 20 min at room temperature (RT). The immobilised CA was washed twice by adding 10 mL of ddH2O. 10 mL of 1.5 M Tris-HCI pH 9.1 and 0.5 mL of 5 M CaCI2 were added to the immobilised CAs. The tubes were incubated in the water bath set to 60°C for 15 min in the fume hood. A small piece of dry ice was added to each tube. The reaction was allowed to proceed until the dry ice fumes stopped being released from the tubes. The tubes were incubated in the shaking incubator for 5 min (set to 37°C). The tubes were then centrifuged for 1 min at 4,300 x ref. The supernatant was decanted from the tubes and the carbonate content was measured using the Calcimeter. | [0408] The outcome of the experiment is shown in Figure 9, which shows that Remin basalt (Rb) performed comparably to silica gel (SG) in terms of CO2 sequestration. | [0409] Example 13 | [0410] This example compares the effect of buffer and tap water on the CA reaction. | [0411] Method: 1 mL of CA obtained commercially was mixed with 10 g of either Remin basalt (Remin) or Duntilland basalt (Duntilland) or Tata steel slag (Steel slag) in a 50 mL Falcon tube. The Dentilland basalt and Tata steel slag both had particles with broad size up to 4000 micrometre. 10 mL of 1.5 M Tris pH 9.1 buffer was added to each tube. The tubes were incubated on a rotor for 20 min at room temperature (RT). The immobilised CA was washed twice by adding 10 mL of ddH2O. 10 mL of 1.5 M Tris-HCI pH 9.1 or 10-mL tap water was added to the immobilised CAs. 0.5 mL of 5 M CaCI2 was added to all the Falcon tubes. The tubes were incubated in the water bath set to 60°C for 15 min in the fume hood. A small piece of dry ice was added to each tube. The reaction was allowed to proceed until the dry ice fumes stopped being released from the tubes. The tubes were incubated in the shaking incubator for 5 min (set to 37°C). The tubes were centrifuged for 1 min at 4,300 x ref. The supernatant was decanted from the tubes and the carbonate content was measured using the Calcimeter.The outcome of the experiment is shown in Figure 10, which shows that tap water had considerable impact on CO2 sequestration. This is most likely due to the presence of divalent cations in the tap water, which are known to enhance carbonic anhydrase activity. Furthermore, steel slag was shown to have comparable performance to that of Remin basalt. | [0412] Example 14 | [0413] This example demonstrates onboarding of basalt sourced from Crag Mill. | [0414] Method: 1 mL of CA obtained commercially was mixed with 10 g of either Remin basalt (Remin) or Duntilland basalt (Duntilland) or Crag Mill basalt in a 50 mL Falcon tube. The Dentilland basalt and Crag Mill basalt both had particles with broad size up to4000 micrometre. 10 mL of tap water was added to each tube. The tubes were incubated on the rotor for 20 min at room temperature (RT). The immobilised CA was washed twice by adding 10 mL of tap water. 10 mL of tap water and 0.5 mL of 5 M CaCI2 were added to each tube. The tubes were incubated in the water bath set to 60°C for 15 min in the fume hood. A small piece of dry ice was added to each tube. The reaction was allowed to proceed until the dry ice fumes stopped being released from the tubes. The tubes were incubated in the shaking incubator for 5 min (set to 37°C). The tubes were then centrifuged for 1 min at 4,300 x ref. The supernatant was decanted from the tubes and the carbonate content was measured using the Calcimeter. | [0415] The outcome of the experiment is shown in Figure 11 , which shows that the absolute % CO2 equivalent captured using Crag Mill basalt is comparable to that captured using Dentilland basalt. However, the percentage improvement attained by adding enzymes to the basalt is highest at 125% compared to 67% and 7.5% for Remin basalt and Dentilland basalt, respectively. | [0416] Example 15 | [0417] This example demonstrates the effect of temperature, pressure, longer immobilization, and combination of increased pressure and temperature on the performance of CA immobilized on Dentilland basalt. | [0418] Method: 1 mL of CA obtained commercially was mixed with 10 g of Duntilland basalt (particle size up to 4000 micrometre) in each of 50 mL Falcon tubes 1 , 2, 3, and 4. 10 mL of tap water was added to each tube. T ubes 1 ,2, and 4 were incubated on the rotor for 20 min at RT, while tube 3 was incubated for 24 h. The immobilised CA was washed twice by adding 10 mL of tap water. 10 mL tap water and 0.5 mL of 5 M CaCI2 were added to the immobilised CAs. Each of the tubes were incubated in the water bath set to 60°C for 15 min in the fume hood. 2.5g of dry ice was added to each tube. The reaction was allowed to proceed until the dry ice fumesstopped being released from tubes 1 and 3. For tubes 2 and 4, dry ice fumes were trapped in the falcon to increase the pressure. Tubes 2 and 3 were incubated at 37°C, while tubes 1 and| [0419] 4 were incubated at 47°C for 5 minutes in a shaker incubator. The tubes were centrifuged for 1 min post reaction at 4,300 x ref. The supernatant was decanted from the tubes and the carbonate content was measured using the Calcimeter. | [0420] The outcome of the experiment is shown in Figure 12, which shows that the kinetic process conditions such as temperature, pressure did not influence the reaction performance of immobilized CA. Additionally, longer immobilization did not increase the enzyme loading or the CO2 capture. | [0421] Example 16 | [0422] This example demonstrates the effect of long-term CO2 exposure. | [0423] Method: 1 mL of CA obtained commercially or 1 mL water for control reaction was mixed with| [0424] 5 g of Duntilland basalt (particle size up to 4000 micrometre) in a 10 mL packed bed reactor. 10 mL of tap water was added to each reactor. The reactors were incubated for 60 min at room temperature (RT). CO2 gas was fed into the reactors for 23 h at 0.5 bars using a pressure regulator. To avoid dehydration by CO2, the CO2 was bubbled through water. The basalt was decanted into a clean Petri dish and the carbonate content was measured using the Calcimeter. | [0425] The outcome of this experiment is shown in Figure 13, which shows that the flow of CO2 increases the residence time and the mass transfer co-efficient. This improves the CO2 sequestration by 13x. | [0426] Example 17 | [0427] This example demonstrates immobilization efficiency and leaching of CA on Dentilland basalt. Method: 1 mL of CA obtained commercially was mixed with 10 g of Duntilland basalt in a 50 mL Falcon tube. 10 mL of tap water was added to the tube. The tube was incubated on the rotor for 20 min at room temperature (RT). The immobilised CA was washed twice by adding 10 mL of tap water. The supernatant post immobilization and the wash fractions were collected for later analysis. 10 mL of tap water and 0.5 mL of 5 M CaCI2 were added to the immobilised CAs. The reaction tube was incubated in the water bath set to 60°C for 15 min in the fume hood. 1g of dry ice was added to the tube. The reaction was allowed to proceed until the dry ice fumes stopped being released and the tube was incubated at 37°C for 5 minutes in a shaker incubator. After the reaction, the tube was centrifuged for 1 min post reaction at 4,300 x refand the supernatant fraction was collected. The enzyme activity of all the fractions was determined using 4-NPA assay and compared with the fresh enzyme of same dilution. | [0428] Carbonic anhydrase is bound to basalt using non-specific ionic interactions. The outcome of the experiment is shown in Figure 14. | [0429] Example 18 | [0430] This example demonstrates the results obtained from pre-trials in open field. | [0431] Method: Water permeable membrane was spread on grass land. 36 plots of 2m by 2m were measured and marked with ropes. 16 kg of Dentilland basalt or Remin basalt was added to 50 L water and the content was poured in the centre of the grid. The basalt was spread over the grid to form a layer. The bio-actives shown in Table 3 were sprayed at the required concentration of the respective grid. Samples were taken weekly on days on which precipitation did not occur. Approximately 50 g of basalt was scooped into a 50 mL falcon for sampling. The in situ pH probe was used to measure the pH in parallel during sampling. The residual enzyme activity was measured using the 4NPA assay and the carbonate content was measured using a Calcimeter. | [0432] Table 3 The different bio actives used in the pre-trial.| [0433] | [0434] The outcome of the experiment is shown in Figures 15A, 15B and 15C. | [0435] The pH measurements of the soil are shown in Table 3. These pH measurements were obtained when the soil temperature was 8.3°C, when there had been no precipitation for at least 24 hours, and were taken on day X12 after application of each CA source to the respective plot. Corresponding alpha, beta, gamma and delta plots, with Remin basalt, measured on day 12, were pH 6.2, 5.3, 6.2, and 5.9, respectively. The four control plots (without basalt and enzyme), measured on day 12, were pH 6, 6, 6.1 , and 6.2. | [0436] It was observed the CA obtained commercially along with Kefir, Yakult and baker’s yeast show relative increase in the CO2 equivalent measured using a Calcimeter, which indicated the presence of active CA and improved CO2 sequestration. | [0437] It is understood that the examples and embodiments described herein are for illustrative purposes only and that various modifications or changes in light thereof will be suggested to persons skilled in the art and are to be included within the spirit and purview of this application and scope of the appended claims. All publications, sequence accession numbers, patents, and patent applications cited herein are hereby incorporated by reference in their entirety for all purposes. Family Number|(111678262)|111678262|Abstract|(WO2024201086 A1)|This invention relates to carbon sequestration, in particular by enhanced weathering. The methods generally utilise an enzyme, typically carbonic anhydrase. In particular, the invention relates to methods of sequestering atmospheric carbon by applying Carbonic Anhydrase, and optionally rock, to soil or earth. An immobilsied enzyme is also provided, along with the use of that enzyme to sequester atmospheric carbon. Mixtures comprising carbonic anhydrase are also provided, for example carbonic anhydrase mixed with one or more of soil, seed and rock.|(EP4587163 A1)|This invention relates to carbon sequestration, in particular by enhanced weathering. The methods generally utilise an enzyme, typically carbonic anhydrase. In particular, the invention relates to methods of sequestering atmospheric carbon by applying Carbonic Anhydrase, and optionally rock, to soil or earth. An immobilsied enzyme is also provided, along with the use of that enzyme to sequester atmospheric carbon. Mixtures comprising carbonic anhydrase are also provided, for example carbonic anhydrase mixed with one or more of soil, seed and rock.|CPC codes|(WO2024201086 A1)|A01G-024/12|A01G-024/22|B01D-053/62|B01D-053/85|B01D-2251/402|B01D-2251/404|B01D-2255/804|B01D-2257/504|B01D-2258/06|(EP4587163 A1)|A01G-024/12|A01G-024/22|B01D-053/62|B01D-053/85|B01D-2251/402|B01D-2251/404|B01D-2255/804|B01D-2257/504|B01D-2258/06|IPC codes|(WO2024201086 A1)|A01G-022/00|A01G-024/15|B01D-053/62|B01D-053/85|(EP4587163 A1)|A01G-022/00|A01G-024/15|B01D-053/62|B01D-053/85|(BR112025016082 A0)|A01G-022/00|A01G-024/15|B01D-053/62|B01D-053/85|(HK40129248 A)|A01G-022/00|A01G-024/15|B01D-053/62|B01D-053/85| Biotechnology|Environmental technology|Other special machines A01G-024/12|A01G-024/22|B01D-053/62|B01D-053/85|B01D-2251/402|B01D-2251/404|B01D-2255/804|B01D-2257/504|B01D-2258/06|C12N-009/88|C12N-011/02|C12N-011/14|C12Y-402/01001 A01G-024/12|A01G-024/22|B01D-053/62|B01D-053/85|B01D-2251/402|B01D-2251/404|B01D-2255/804|B01D-2257/504|B01D-2258/06|C12N-009/88|C12N-011/02|C12N-011/14|C12Y-402/01001 A01G-022/00|A01G-024/15|B01D-053/62|B01D-053/85|C12N-009/00|C12N-011/14|C12N-011/16|C12P-003/00 A01G-022/00|A01G-024/15|B01D-053/62|B01D-053/85|C12N-009/00|C12N-011/14|C12N-011/16|C12P-003/00 WO2022197596|US20220132865|WO202287289 WO2022197596 101871974 WHO=Examiner SELF=N CAT=X CAT=I|US20220132865 99806202 WHO=Examiner SELF=N CAT=X CAT=I|WO202287289 107406107 WHO=Examiner SELF=N CAT=X CAT=I WO202287289; XP036851424; US20220132865; WO2022197596||| |(WO2024/201086)|International Search Report [Examiner]|-NATHAN VINOD KUMAR ET AL: "Carbon Dioxide Sequestering Ability of Bacterial Carbonic Anhydrase in a Mangrove Soil Microcosm and Its Bio-mineralization Properties", WATER, AIR, SPRINGER INTERNATIONAL PUBLISHING, CHAM, vol. 230, no. 8, 2 August 2019 (2019-08-02), pages 1 - 12, XP036851424, ISSN: 0049-6979, [retrieved on 20190802], DOI: 10.1007/S11270-019-4229-3|-OLIVEIRA MACIEL ET AL., CHEMOSPHERE, vol. 299, no. 134419, July 2022 (2022-07-01), pages 1 - 25|-REN ET AL., COLLOIDS AND SURFACES B: BIOTERFACES, vol. 204, no. 111779, August 2021 (2021-08-01), pages 1 - 10|-WALKLEY ABLACK IA: "An examination of the Degtjareff method for determining soil organic matter, and a proposed modification of the chromic acid titration method", SOIL SCIENCE, vol. 37, 1934, pages 29 - 38|-SHANK ET AL., CHEMICAL BIOLOGY &amp; DRUG DESIGN, vol. 68, no. 2, 2006, pages 113 - 119||| PENDING (EP4587163)|PENDING|(WO2024/201086)|PENDING|(HK40129248)|PENDING|(BR112025016082)|PENDING ALIVE (EP4587163)|ALIVE|(WO2024/201086)|ALIVE|(HK40129248)|ALIVE|(BR112025016082)|ALIVE (EP4587163)|LEGAL DETAILS FOR EP4587163|Actual or expected expiration date=2044-04-02|Legal state=ALIVE|Status=PENDING|Event publication date=2024-04-02|Event code=EP/APP|Event indicator=Pos|Event group=Examination events|Application details|Application 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GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML|(WO2024/201086)|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (EP4587163)|EP; HK|(WO2024/201086)|WO; BR; EP; HK|(HK40129248)|HK|(BR112025016082)|BR https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=nwH/nfofj490Km40DIbS1qCa4vFyxJplNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006593519&ekey=2120&xpn=EP4587163&kind=A1 https://register.epo.org/application?number=EP24719614 https://permalink.orbit.com/RenderStaticFirstPage?XPN=mXvk71Xl%252FtueccOAsqvWAnfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT GB (WO2024/201086)|GB (WO2024/201086)|NAME=FABRICNANO LIMITED 9th Floor 107 Cheapside London Greater London EC2V 6DN , COUNTRY=GB (EP4587163)|GB|(WO2024/201086)|GB|(HK40129248)|HK (EP4587163)|NAME=Elkington and Fife LLP;Prospect House 8 Pembroke Road , CITY=Sevenoaks, Kent TN13 1XR , COUNTRY=GB , REG=101770561|(WO2024/201086)|NAME=ELKINGTON AND FIFE LLP Prospect House 8 Pembroke Road Sevenoaks Kent TN13 1XR , POSTCODE=TN13 1XR , COUNTRY=GB|(HK40129248)|NAME=WENPING PATENT & TRADE MARK AGENT LIMITED , COUNTRY=HK (EP4587163)|GB; GB; GB|(WO2024/201086)|GB; GB; GB| (EP4587163)|NAME=AARONS, Grant, CITY=London, Greater London EC2V 6DN, COUNTRY=GB |NAME=BURNS, Jonathan, CITY=London, Greater London EC2V 6DN, COUNTRY=GB |NAME=SRINIVASAMURTHY, Vishnu, CITY=London, Greater London EC2V 6DN, COUNTRY=GB|(WO2024/201086)|NAME=AARONS, Grant FabricNano Limited 9th Floor, 107 Cheapside London Greater London EC2V 6DN, POSTCODE=EC2V 6DN, COUNTRY=GB |NAME=BURNS, Jonathan FabricNano Limited 9th Floor, 107 Cheapside London Greater London EC2V 6DN, POSTCODE=EC2V 6DN, COUNTRY=GB |NAME=SRINIVASAMURTHY, Vishnu FabricNano Limited 9th Floor, 107 Cheapside London Greater London EC2V 6DN, POSTCODE=EC2V 6DN, COUNTRY=GB|(HK40129248)|NAME=AARONS Grant|NAME=BURNS Jonathan|NAME=SRINIVASAMURTHY Vishnu 22 4 Titre: (EP4587163)|Method of sequestering atmospheric carbon Résumé: (EP4587163)|This invention relates to carbon sequestration, in particular by enhanced weathering. The methods generally utilise an enzyme, typically carbonic anhydrase. In particular, the invention relates to methods of sequestering atmospheric carbon by applying Carbonic Anhydrase, and optionally rock, to soil or earth. An immobilsied enzyme is also provided, along with the use of that enzyme to sequester atmospheric carbon. Mixtures comprising carbonic anhydrase are also provided, for example carbonic anhydrase mixed with one or more of soil, seed and rock. 35 Abstract gpt-4o-mini yes The article discusses enhanced weathering methods for carbon sequestration, specifically using carbonic anhydrase and rock, which aligns with the topic's focus on accelerating mineral alteration for CO₂ capture.
37 CN202410273042 CN202410273042 CN118239702 110341563 CN118239702 A 2024-06-25 [CN118239702] 2024-03-11 2024-03-11 2024-06-25 (CN118239702)|2044-03-11 (CN118239702)|Steel slag sensible heat recovery and carbon sequestration modification process (CN118239702)|The invention discloses a steel slag sensible heat recovery and carbon sequestration modification process, which comprises the following steps that a steel slag melt is subjected to ingot casting through an ingot casting device, a cast high-temperature steel slag ingot shell is in a solid state, and an inner core is in a liquid state; the steel slag ingot enters the vertical reactor from a feeding hole in the upper part of the vertical reactor, meanwhile, metallurgical flue gas is introduced from a gas inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, and meanwhile, the high-temperature steel slag ingot reacts with CO2 in the flue gas to form CO2 in the high-temperature flue gas; carrying out carbon sequestration modification on the steel slag ingot to form a carbon sequestration modified steel slag block, and discharging high-temperature flue gas through a pipeline at the top of the vertical reactor; s3, the dedusted high-temperature flue gas enters a heat exchanger for heat exchange, and the flue gas is discharged from a chimney after heat exchange; the carbon sequestration modified steel slag blocks are crushed, separated and then graded for utilization, and high-added-value steel slag products are prepared. And steel slag sensible heat recovery and steel slag carbon sequestration can be performed simultaneously. ANHUI UNIVERSITY OF TECHNOLOGY (CN118239702)|ANHUI UNIVERSITY OF TECHNOLOGY ([CN]) LONG HONGMING|WEI RUFEI|FAN CHUNLONG|SUN RONG|ZHANG HAO|DI ZHANXIA (CN118239702)|LONG HONGMING|WEI RUFEI|FAN CHUNLONG|SUN RONG|ZHANG HAO|DI ZHANXIA (CN118239702)|ZHANG YONGSHENG;ANHUI INTELLECTUAL PROPERTY AGENCY CO LTD|Reg. Nb: 34107 (CN118239702)|Compared with the prior art, the invention has the following advantages:|However, the existing steel slag carbon fixation technology ignores sensible heat recovery of steel slag, and causes a great amount of resource waste.|The invention has the following advantages:|For example, the application of China patent application No. 202223494217.1 discloses a device for efficiently capturing carbon dioxide by activating steel slag, which is characterized in that firstly, the steel slag is crushed, then Ca 2+ is leached into solution by acid leaching, then the liquid enters a CO 2 absorption tower to absorb CO 2, however, the efficiency of indirectly fixing carbon in steel slag leaching is limited by the influence of Ca 2+ leaching rate in steel slag, and the treatment mode has large water consumption and serious environmental pollution.|For example, the application of chinese patent application number 201710117736.0 discloses a method for recycling high-temperature slag, in which the high-temperature liquid slag is quenched and then enters a centrifugal granulator for granulation, and then the resulting granules are subjected to forced heat exchange with water, and then the heat is recovered, but the sensible heat recovery efficiency of the method is relatively low and the slag granules after heat exchange are difficult to treat.|The application of China patent application No. 201811004273.8 discloses a device for mechanical thermal crushing and waste heat recovery of steel slag, which is characterized in that hot steel slag is poured into a charging hopper, cooling water is sprayed, mechanical crushing is carried out, and finally generated high-temperature steam is recovered, but the steel slag produced by a mechanical crushing method is difficult to meet industrial utilization due to uneven size of steel slag particles, and meanwhile, the temperature of the cooled steel slag is still higher (500-900 ℃), so that the sensible heat recovery efficiency of the steel slag is greatly reduced.| (CN118239702)|1. A steel slag sensible heat recovery and carbon fixation modification process is characterized in that: the process comprises the following steps: s1: the steel slag melt is cast by an ingot device, the cast high-temperature steel slag ingot shell is solid, and the inner core is liquid; s2: the steel slag ingot enters the vertical reactor from a feed inlet at the upper part of the vertical reactor through a feeding device, metallurgical flue gas is introduced from an air inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas flows from bottom to top in the vertical reactor, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, the high-temperature steel slag ingot reacts with CO 2 in the flue gas to perform carbon fixation modification on the steel slag ingot to form a carbon fixation modified steel slag block, and the high-temperature flue gas is discharged through a pipeline at the top of the vertical reactor; S3: the flue gas is discharged from the vertical reactor and enters a gravity dust remover for dust removal, the high-temperature flue gas after dust removal enters a heat exchanger for heat exchange, and the flue gas is discharged from a chimney after heat exchange; the carbon-fixing modified steel slag blocks are crushed and separated for grading utilization, so that the steel slag high-added-value product is prepared. | (CN118239702)|Aiming at the defects of the prior art, the invention provides a steel slag sensible heat recovery and carbon fixation modification process, so as to achieve the aim of simultaneously carrying out steel slag sensible heat recovery and steel slag carbon fixation and improving the resource utilization rate.|The invention discloses a steel slag sensible heat recovery and carbon fixation modification process, which comprises the following steps: the steel slag melt is cast by an ingot device, the cast high-temperature steel slag ingot shell is solid, and the inner core is liquid; the steel slag ingot enters the vertical reactor from a feed inlet at the upper part of the vertical reactor, metallurgical flue gas is introduced from an air inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, the high-temperature steel slag ingot reacts with CO 2 in the flue gas to carry out carbon fixation modification on the steel slag ingot to form a carbon fixation modified steel slag block, and the high-temperature flue gas is discharged through a pipeline at the top of the vertical reactor; s3: the high-temperature flue gas after dust removal enters a heat exchanger for heat exchange, and the flue gas after heat exchange is discharged from a chimney; the carbon-fixing modified steel slag blocks are crushed and separated for grading utilization, so that the steel slag high-added-value product is prepared.|The invention relates to the technical field of steel slag sensible heat recovery and carbon fixation, in particular to a steel slag sensible heat recovery and carbon fixation modification process.| (CN118239702)|CARBON FIXATION(100,41)|SLAG SENSIBLE HEAT RECOVERY(100,25)|CARBON FIXATION MODIFICATION(100,10)|CARBON FIXATION MODIFICATION(100,5)|STEEL SLAG INGOT(85,11)|SLAG INGOT(79,22)|SLAG INGOT SHELL(76,4)|STEEL SLAG(70,61)|REACTOR(63,43)|GRADING UTILIZATION(55,4)|STEEL SLAG MELT(53,7)|CARBON SEQUESTRATION MODIFICATION(52,9)|CENTRIFUGAL GRANULATOR(48,1)|SLAG GRANULE(47,1)|STEEL SLAG BLOCK(43,7)|GRAVITY DUST REMOVER(43,3)|FLUE GAS(38,43)|AIR INLET PIPELINE(37,9)|STEEL SLAG LEACHING(37,2)|CHARGING HOPPER(37,1)|CRUSHING(34,6)|ABSORPTION TOWER(34,1)|INGOT(33,4)|COOLED STEEL SLAG(33,1)|METALLURGICAL FLUE GAS(32,8)|CA INFLUENCE(32,1)|RECOVERING SENSIBLE HEAT(30,7)|STEEL HOT SLAG(30,1)|FEED INLET(29,4)|INVERTED TRAPEZOID DISCHARGING PORT(29,2)|PIPELINE(28,8)|FLUE GAS EXCHANGE(28,4)|RESOURCE WASTE(28,3)|STEEL SLAG PARTICLE(28,2)|STEEL SLAG FIX CARBON(28,1)|STEEL SLAG CARBON FIXATION(27,10)|CHIMNEY(27,5)|COOLED STEEL SLAG TEMPERATURE(22,1)|GRANULATION(22,1)|LEACHING RATE(21,1)|GRANULE(20,1)|HEAT EXCHANGE(18,16)|FIXED CARBON(18,2)|FIXING CARBON(18,1)|TREATMENT MODE(17,1)|HEAT EXCHANGER(16,11)|STEEL SLAG SENSIBLE HEAT(16,9)|DUST REMOVAL(16,7)|ENVIRONMENTAL POLLUTION(14,3)|COOLING WATER(14,1)|FORCED HEAT EXCHANGE(14,1)|UNEVEN SIZE(14,1)|CARBON FIXING(12,9)|SEPARATING EQUIPMENT(12,4)|DISCHARGE HOLE(12,3)|ACID LEACHING(12,1)|INNER CORE(11,7)|RESOURCE UTILIZATION RATE(10,3)|AIR OUTLET PIPELINE(9,3)|OUTER SHELL(9,3)|STEEL SLAG CASTING(9,2)|MOLTEN SLAG GRANULE(9,1)|WATER CONSUMPTION(9,1)|FLUE GAS FLOW(8,3)|CARBON DIOXIDE(8,2)|WASTE HEAT RECOVERY(8,1)|SOLID PHASE(7,3)|CARBONATE DECOMPOSITION(7,2)|STEEL SLAG SLURRY(7,2)|CENTRIFUGAL GRANULATION(7,1)|STEEL SLAG GELATION(7,1)|CENTRIFUGAL GRANULATING(6,1)|ECOLOGICAL ENVIRONMENT POLLUTION(6,1)|METALLURGICAL FLUE GAS SOLIDIFICATION(6,1)|RECYCLING HIGH TEMPERATURE SLAG(6,1)|STEEL SLAG CRUSHING(6,1)|HIGH TEMPERATURE FLUE GAS(5,13)|COUNTERCURRENT FLOW(5,2)|INDIRECT CARBON FIXATION(5,2)|CONVERTER STEEL SLAG MELT(5,1)|HUMAN INDUSTRIALIZATION(5,1)|SOIL OCCUPATION(5,1)|STEEL SLAG BRICK(5,1)|STEEL SLAG RECYCLING(5,1)|THROWING TRAY(5,1)|WINE HEART CHOCOLATE(5,1)|CARBONATION(4,2)|DISSOLVING CALCIUM(4,1)|ROTARY DRUM(4,1)|SLAG TAPPING TEMPERATURE(4,1)|STEEL SLAG POWDER(4,1)|STEEL SLAG STABILITY(4,1)|SYSTEMATIC RESEARCH(4,1)|ULTIMATE RECOVERY(4,1)|WET MILLED STEEL SLAG(4,1)|GAS PHASE(3,3)|ENTERPRISE(3,2)|SIGNIFICANCE(3,2)|CHARGING BOX(3,1)|CRUSHING EQUIPMENT(3,1)|DISCHARGING PORT(3,1)|HIGH TEMPERATURE LIQUID SLAG(3,1)|HIGH TEMPERATURE STEAM(3,1)|MODIFIED STEEL SLAG(3,1)| (CN118239702)|1. A steel slag sensible heat recovery and carbon fixation modification process is characterized in that: the process comprises the following steps:| s1: the steel slag melt is cast by an ingot device, the cast high-temperature steel slag ingot shell is solid, and the inner core is liquid; | s2: the steel slag ingot enters the vertical reactor from a feed inlet at the upper part of the vertical reactor through a feeding device, metallurgical flue gas is introduced from an air inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas flows from bottom to top in the vertical reactor, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, the high-temperature steel slag ingot reacts with CO 2 in the flue gas to perform carbon fixation modification on the steel slag ingot to form a carbon fixation modified steel slag block, and the high-temperature flue gas is discharged through a pipeline at the top of the vertical reactor; | S3: the flue gas is discharged from the vertical reactor and enters a gravity dust remover for dust removal, the high-temperature flue gas after dust removal enters a heat exchanger for heat exchange, and the flue gas is discharged from a chimney after heat exchange; the carbon-fixing modified steel slag blocks are crushed and separated for grading utilization, so that the steel slag high-added-value product is prepared. |2. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 1, wherein: the temperature range of the steel slag melt is 1500-1700 ℃.|3. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 1, wherein: the temperature range of the cast high-temperature steel slag ingot is 900-1300 ℃.|4. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 1, wherein: the gas phase and the solid phase in the vertical reactor adopt countercurrent flow.|5. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 1, wherein: the feeding port of the vertical reactor is arranged on one side of the upper part of the vertical reactor, the air inlet pipeline is positioned on one side of the lower part, the bottom is an inverted trapezoid discharging port, and the center of the top is provided with an air outlet pipeline.|6. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 1, wherein: the temperature range of the flue gas discharged from the pipeline at the top of the vertical reactor is 700-1100 ℃.|7. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 1, wherein: the heat exchanger is a vertical heat exchanger.|8. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 3, wherein: the temperature of the outer shell of the high-temperature steel slag ingot is 850-900 ℃, and the temperature of the inner core of the high-temperature steel slag ingot is 1250-1300 ℃.|9. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 5, wherein: the two air inlet pipelines are symmetrically arranged on two sides of the lower part of the vertical reactor.|10. The steel slag sensible heat recovery and carbon sequestration modification process according to claim 5, wherein: the lower part of the vertical reactor is provided with a conveying mechanism corresponding to the discharge hole, and crushing equipment and separating equipment are sequentially arranged behind the conveying mechanism. (CN118239702)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of steel slag sensible heat recovery and carbon fixation, in particular to a steel slag sensible heat recovery and carbon fixation modification process.|BACKGROUND ART|[0002] With the development and progress of human industrialization, the emission amount of CO 2 is continuously increased, and thus the global warming problem is increasingly serious, and how to reduce carbon emission and suppress global warming is a hot spot of human interest.|[0003] The slag tapping temperature of the steel slag is up to 1400-1600 ℃, the specific heat capacity in the molten state is about 1.2 kJ/(kg·DEG C), and 1 ton of steel slag can recover about 1.2GJ of sensible heat calculated by the initial temperature of 1400 ℃ and the end temperature of 500 ℃, which is equivalent to the heat generated when 41kg of standard coal is completely combusted. For the steel slag sensible heat recovery technology developed at present, the crushing of the steel slag is an indispensable step, and three common physical methods are promoted on the basis of the crushing mechanism: mechanical crushing, air quenching and centrifugal granulating.|[0004] The mechanical crushing method comprises a solid particle impact method, a mechanical stirring method and a rotary drum method, and the molten steel slag is decomposed into steel slag particles mainly by mechanical force. The application of China patent application No. 201811004273.8 discloses a device for mechanical thermal crushing and waste heat recovery of steel slag, which is characterized in that hot steel slag is poured into a charging hopper, cooling water is sprayed, mechanical crushing is carried out, and finally generated high-temperature steam is recovered, but the steel slag produced by a mechanical crushing method is difficult to meet industrial utilization due to uneven size of steel slag particles, and meanwhile, the temperature of the cooled steel slag is still higher (500-900 ℃), so that the sensible heat recovery efficiency of the steel slag is greatly reduced.|[0005] The air quenching method adopts high-speed high-pressure gas to impact the molten steel slag flow, and the slag is decomposed into small particles while being rapidly cooled. The application number 201210387654.5 discloses equipment and a method for quenching liquid steel slag and recycling waste heat, wherein the application number is 201210387654.5, the liquid steel slag is quenched and cracked into uniform particles by adopting low-temperature nitrogen, and the waste heat is recycled by pneumatic conveying.|[0006] The centrifugal granulation method is to granulate the molten slag by centrifugal force, thereby creating conditions for recovering sensible heat. For example, the application of chinese patent application number 201710117736.0 discloses a method for recycling high-temperature slag, in which the high-temperature liquid slag is quenched and then enters a centrifugal granulator for granulation, and then the resulting granules are subjected to forced heat exchange with water, and then the heat is recovered, but the sensible heat recovery efficiency of the method is relatively low and the slag granules after heat exchange are difficult to treat.|[0007] The steel slag is taken as typical metallurgical industry solid waste, is mainly used for preparing cement, road materials, steel slag bricks and the like, and has the problems of low stability, low gelation activity and the like of free calcium oxide, so that the comprehensive utilization rate of the steel slag is lower than 30 percent, the steel slag storage amount is more than 10 hundred million t, and the problems of land occupation, ecological environment pollution and the like are caused. But the steel slag is rich in calcium and magnesium, usually contains 40% -60% of CaO and 2% -10% of MgO, has remarkable carbonation effect, can absorb CO 2, replaces natural ores to trap and seal CO 2, and reduces carbon emission. at present, the carbon fixation of the steel slag can be divided into indirect carbon fixation by leaching and direct carbon fixation by thermal state. The indirect carbon fixation of the steel slag leaching is generally carried out by dissolving Ca 2+ in the steel slag by solution under the condition that the temperature is less than 200 ℃, then reacting with CO 32- in the solution to generate CaCO 3, thereby achieving the aim of indirectly fixing carbon. For example, the application of China patent application No. 202223494217.1 discloses a device for efficiently capturing carbon dioxide by activating steel slag, which is characterized in that firstly, the steel slag is crushed, then Ca 2+ is leached into solution by acid leaching, then the liquid enters a CO 2 absorption tower to absorb CO 2, however, the efficiency of indirectly fixing carbon in steel slag leaching is limited by the influence of Ca 2+ leaching rate in steel slag, and the treatment mode has large water consumption and serious environmental pollution. The thermal state direct carbon fixation is to carry out carbon fixation treatment when the steel slag is at high temperature, so that the dual purposes of steel slag carbon fixation and sensible heat utilization can be achieved, the carbon fixation efficiency of the steel slag is improved in the high temperature state, and carbonate products are also generated, so that the compactness and compressive strength of the steel slag structure are improved, the gelation activity of the steel slag is improved, the contents of f-CaO and f-MgO can be reduced, the stability of the steel slag is improved, and the recycling value of the steel slag is improved.|[0008] However, the existing steel slag carbon fixation technology ignores sensible heat recovery of steel slag, and causes a great amount of resource waste. The application number 202211142705.8 discloses a steel slag carbon fixing device and a use method thereof, wherein steel slag powder is added into a charging box, and is thrown out through a throwing tray, so that the steel slag powder reacts with CO 2 to generate carbonate for carbon fixing, and sensible heat of the steel slag is not recovered while carbon fixing. Another example is the application of chinese patent application number 202210599827.3, which discloses a method for carbon sequestration and emission reduction of wet-milled steel slag in steel works, and application thereof, wherein the application is to quench the molten steel slag produced in the steel works by water quenching, then crush, remove iron and dry the molten steel slag in sequence to obtain steel slag powder, then prepare the steel slag powder into steel slag slurry, and finally use the steel slag slurry to conduct carbon sequestration. However, the application directly quenches and quenches the molten steel slag produced by the steel plant, and the sensible heat of the steel slag is wasted.|[0009] Because the steel slag generated by the steel plant is in a molten liquid state, the temperature is higher (more than 1500 ℃), the sensible heat of the steel slag is difficult to realize by gas-liquid heat exchange, and the gas-solid heat exchange has the highest efficiency, but the complete casting of the steel slag into a solid state can cause the loss of most sensible heat of the steel slag, so that the resource waste is caused. Reducing CO2 emission, steel slag sensible heat recovery and steel slag recycling have become the problems to be solved urgently in the metallurgical industry at present.|DISCLOSURE|Disclosure of Invention|[0010] Aiming at the defects of the prior art, the invention provides a steel slag sensible heat recovery and carbon fixation modification process, so as to achieve the aim of simultaneously carrying out steel slag sensible heat recovery and steel slag carbon fixation and improving the resource utilization rate.|[0011] In order to solve the technical problems, the invention adopts the following technical scheme:|[0012] the steel slag sensible heat recovery and carbon fixation modification process comprises the following steps: |[0013] s1: the steel slag melt is cast by an ingot device, the cast high-temperature steel slag ingot shell is solid, and the inner core is liquid; |[0014] s2: the steel slag ingot enters the vertical reactor from a feed inlet at the upper part of the vertical reactor through a feeding device, metallurgical flue gas is introduced from an air inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas flows from bottom to top in the vertical reactor, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, the high-temperature steel slag ingot reacts with CO 2 in the flue gas to perform carbon fixation modification on the steel slag ingot to form a carbon fixation modified steel slag block, and the high-temperature flue gas is discharged through a pipeline at the top of the vertical reactor; |[0015] S3: the flue gas is discharged from the vertical reactor and enters a gravity dust remover for dust removal, the high-temperature flue gas after dust removal enters a heat exchanger for heat exchange, and the flue gas is discharged from a chimney after heat exchange; the carbon-fixing modified steel slag blocks are crushed and separated for grading utilization, so that the steel slag high-added-value product is prepared. |[0016] Wherein,|[0017] The temperature range of the steel slag melt is 1500-1700 ℃.|[0018] The temperature range of the cast high-temperature steel slag ingot is 900-1300 ℃.|[0019] The gas phase and the solid phase in the vertical reactor adopt countercurrent flow.|[0020] The feeding port of the vertical reactor is arranged on one side of the upper part of the vertical reactor, the air inlet pipeline is positioned on one side of the lower part, the bottom is an inverted trapezoid discharging port, and the center of the top is provided with an air outlet pipeline.|[0021] The temperature range of the flue gas discharged from the pipeline at the top of the vertical reactor is 700-1100 ℃.|[0022] The heat exchanger is a vertical heat exchanger.|[0023] The temperature of the outer shell of the high-temperature steel slag ingot is 850-900 ℃, and the temperature of the inner core of the high-temperature steel slag ingot is 1250-1300 ℃.|[0024] The two air inlet pipelines are symmetrically arranged on two sides of the lower part of the vertical reactor.|[0025] The lower part of the vertical reactor is provided with a conveying mechanism corresponding to the discharge hole, and crushing equipment and separating equipment are sequentially arranged behind the conveying mechanism.|[0026] Compared with the prior art, the invention has the following advantages:|[0027] The steel slag sensible heat recovery and carbon fixation modification process is reasonable in design, can simultaneously perform steel slag sensible heat recovery and steel slag carbon fixation, overcomes the difficulty that steel slag sensible heat recovery and steel slag carbon fixation are difficult to simultaneously perform in the prior art, improves the utilization rate of resources, reduces the running cost of enterprises, can effectively alleviate the environmental pollution problem caused by steel slag, and has important significance for the high-quality development of the metallurgical industry. |DRAWINGS DESCRIPTION|[0028] The contents and the marks in the drawings expressed in the drawings of the present specification are briefly described as follows:|[0029] FIG. 1 is a schematic diagram of the process flow of the present invention. |INVENTION MODE|Detailed Description|[0030] The following description of the embodiments of the present invention refers to the accompanying drawings, which illustrate in further detail.|[0031] The steel slag sensible heat recovery and carbon fixation modification process comprises the steps of firstly casting steel slag into blocks, wherein the cast blocks have the structural characteristics of 'wine-heart chocolate', namely, the shell is in a low-temperature solid state, the inner core is in a high-temperature liquid state, and the structure can recover the steel slag sensible heat to the greatest extent; then, the steel slag ingot is conveyed into a vertical reactor to exchange heat with metallurgical flue gas, and simultaneously the steel slag ingot reacts with carbon dioxide in the flue gas to carry out carbon fixation modification on the steel slag; and finally, recycling the steel slag after carbon fixation modification.|[0032] The process can simultaneously perform steel slag sensible heat recovery and steel slag carbon fixation, overcomes the difficulty that the steel slag sensible heat recovery and the steel slag carbon fixation are difficult to simultaneously perform in the prior art, improves the utilization rate of resources, reduces the running cost of enterprises, can effectively relieve the environmental pollution problem caused by the steel slag, and has important significance for the high-quality development of the metallurgical industry.|[0033] The preferred specific examples shown in fig. 1 are:|[0034] the slag sensible heat recovery and carbon fixation modification process based on slag ingots comprises the following steps of: |[0035] s1: the steel slag melt produced by the steel plant is cast by an ingot device, the cast high-temperature steel slag ingot has solid outer shell and liquid inner core; |[0036] S2: the high-temperature steel slag ingot enters the vertical reactor from a feed inlet at the upper part of the vertical reactor through a feeding device, metallurgical flue gas is introduced from an air inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas flows from bottom to top in the vertical reactor, the metallurgical flue gas flows reversely with the high-temperature steel slag ingot, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, the high-temperature steel slag ingot reacts with CO 2 in the flue gas to perform carbon fixation modification on the steel slag ingot, and the high-temperature flue gas is discharged through a pipeline at the top of the vertical reactor; |[0037] S3: the high-temperature flue gas is discharged from the vertical reactor and enters a gravity dust remover for dust removal, the high-temperature flue gas after dust removal enters a heat exchanger for heat exchange, and the flue gas after heat exchange is discharged from a chimney. The carbon-fixing modified steel slag blocks are crushed and separated for grading utilization, so that the steel slag high-added-value product is prepared. |[0038] Wherein,|[0039] The temperature range of the steel slag melt is 1500-1700 ℃; the temperature range of the cast high-temperature steel slag ingot is 900-1300 ℃, and the shape of the cast high-temperature steel slag ingot can be square, cuboid, arc-shaped side and cylinder, the outer shell temperature is 850-900 ℃, and the inner core temperature is 1250-1300 ℃.|[0040] The feeding port at the upper part of the vertical reactor is arranged at one side of the vertical reactor, the lower part is provided with two air inlet pipelines which are respectively symmetrically arranged at the left side and the right side, the bottom is inverted trapezoid and is provided with a discharging port, and the center of the top is provided with an air outlet pipeline; the temperature range of the flue gas discharged from the pipeline at the top of the vertical reactor is 700-1100 ℃.|[0041] The heat exchanger is a vertical heat exchanger; the vertical reactor, the gravity dust remover, the heat exchanger and the chimney are all connected by pipelines. The lower part of the vertical reactor is provided with a conveying mechanism corresponding to the discharge hole, and crushing equipment and separating equipment are sequentially arranged behind the conveying mechanism, wherein the crushing equipment and the separating equipment can adopt the existing equipment.|[0042] Because the steel slag generated by the steel plant is in a molten liquid state, the temperature is higher (more than 1500 ℃), the sensible heat of the steel slag is difficult to realize by gas-liquid heat exchange, and the gas-solid heat exchange has the highest efficiency, but the complete casting of the steel slag into a solid state can cause the loss of most sensible heat of the steel slag, so that the resource waste is caused. Aiming at the problem, the applicant creatively provides a high-temperature steel slag ingot with the structural characteristic of the chocolate with wine centers, and the steel slag ingot has the outer shell in a low-temperature solid state and the inner core in a high-temperature liquid state.|[0043] The applicant carries out systematic research on the carbon fixation characteristics of steel slag and metallurgical flue gas of a steel plant, and discovers that the reaction temperature has great influence on the direct carbon fixation of the steel slag. The carbon fixation reaction does not substantially occur at 500 ℃, and when the temperature is 650 ℃ or higher, the obvious carbon fixation reaction occurs, but at 950 ℃ the concentration of CO 2 starts to rise with the extension of time, which indicates that the carbonate is decomposed again. In order to solve the problem, the applicant proposes a structural design of the vertical reactor, wherein the design adopts gas-solid countercurrent, so that the carbon-fixing reaction fully occurs in a low-temperature region, the decomposition of carbonate in a high-temperature region is avoided, and the high-temperature steel slag ingot is fully reacted in the vertical reactor.|[0044] The invention carries out the industrial experiments of sensible heat recovery and carbon fixation of the converter steel slag; the specific embodiment is as follows:|[0045] The temperature of the converter steel slag melt is 1550 ℃, the temperature of the cast high-temperature steel slag ingot shell is 870 ℃, the temperature of the cast high-temperature steel slag ingot inner core is 1280 ℃, the residence time of the steel slag ingot in the vertical reactor is 1.8h, the temperature of the carbon-fixing modified steel slag is 58 ℃ after carbon fixing and heat exchange, the carbon-fixing conversion rate is up to 92%, the temperature of high-temperature flue gas input by the vertical reactor is 960 ℃, and the sensible heat recovery rate of the steel slag is up to 75%; the method can simultaneously recover the sensible heat of the steel slag and fix the carbon of the steel slag, and overcomes the difficulty that the sensible heat recovery of the steel slag and the carbon fixation of the steel slag are difficult to simultaneously carry out in the prior art. |[0046] The invention has the following advantages:|[0047] 1. By casting the molten steel slag, the shell of the casting is in a low-temperature solid state, and the shell is in a high-temperature liquid state, so that the structure can realize solid conveying of slag, liquid heat exchange of solid steel slag and greatly improve the sensible heat recovery rate of steel slag; 2. the structural design of the vertical reactor is provided, and the gas phase and the solid phase in the vertical reactor flow reversely, so that the carbon fixation reaction fully occurs in a low temperature area, the decomposition of carbonate in a high temperature area is avoided, and the direct carbon fixation efficiency of the steel slag is greatly improved; 3. the ultimate recovery of the sensible heat of slag can be realized, the direct solidification of metallurgical flue gas CO 2 can be realized, the steel slag can be modified through carbonation, and the modified steel slag can be used for high added value. |[0048] While the invention has been described above with reference to the accompanying drawings, it will be apparent that the invention is not limited to the above embodiments, but is capable of being modified or applied to other applications without any modification, as long as the inventive concept and technical scheme are adopted. (CN118239702)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of steel slag sensible heat recovery and carbon fixation, in particular to a steel slag sensible heat recovery and carbon fixation modification process.|BACKGROUND ART|[0002] With the development and progress of human industrialization, the emission amount of CO 2 is continuously increased, and thus the global warming problem is increasingly serious, and how to reduce carbon emission and suppress global warming is a hot spot of human interest.|[0003] The slag tapping temperature of the steel slag is up to 1400-1600 ℃, the specific heat capacity in the molten state is about 1.2 kJ/(kg·DEG C), and 1 ton of steel slag can recover about 1.2GJ of sensible heat calculated by the initial temperature of 1400 ℃ and the end temperature of 500 ℃, which is equivalent to the heat generated when 41kg of standard coal is completely combusted. For the steel slag sensible heat recovery technology developed at present, the crushing of the steel slag is an indispensable step, and three common physical methods are promoted on the basis of the crushing mechanism: mechanical crushing, air quenching and centrifugal granulating.|[0004] The mechanical crushing method comprises a solid particle impact method, a mechanical stirring method and a rotary drum method, and the molten steel slag is decomposed into steel slag particles mainly by mechanical force. The application of China patent application No. 201811004273.8 discloses a device for mechanical thermal crushing and waste heat recovery of steel slag, which is characterized in that hot steel slag is poured into a charging hopper, cooling water is sprayed, mechanical crushing is carried out, and finally generated high-temperature steam is recovered, but the steel slag produced by a mechanical crushing method is difficult to meet industrial utilization due to uneven size of steel slag particles, and meanwhile, the temperature of the cooled steel slag is still higher (500-900 ℃), so that the sensible heat recovery efficiency of the steel slag is greatly reduced.|[0005] The air quenching method adopts high-speed high-pressure gas to impact the molten steel slag flow, and the slag is decomposed into small particles while being rapidly cooled. The application number 201210387654.5 discloses equipment and a method for quenching liquid steel slag and recycling waste heat, wherein the application number is 201210387654.5, the liquid steel slag is quenched and cracked into uniform particles by adopting low-temperature nitrogen, and the waste heat is recycled by pneumatic conveying.|[0006] The centrifugal granulation method is to granulate the molten slag by centrifugal force, thereby creating conditions for recovering sensible heat. For example, the application of chinese patent application number 201710117736.0 discloses a method for recycling high-temperature slag, in which the high-temperature liquid slag is quenched and then enters a centrifugal granulator for granulation, and then the resulting granules are subjected to forced heat exchange with water, and then the heat is recovered, but the sensible heat recovery efficiency of the method is relatively low and the slag granules after heat exchange are difficult to treat.|[0007] The steel slag is taken as typical metallurgical industry solid waste, is mainly used for preparing cement, road materials, steel slag bricks and the like, and has the problems of low stability, low gelation activity and the like of free calcium oxide, so that the comprehensive utilization rate of the steel slag is lower than 30 percent, the steel slag storage amount is more than 10 hundred million t, and the problems of land occupation, ecological environment pollution and the like are caused. But the steel slag is rich in calcium and magnesium, usually contains 40% -60% of CaO and 2% -10% of MgO, has remarkable carbonation effect, can absorb CO 2, replaces natural ores to trap and seal CO 2, and reduces carbon emission. at present, the carbon fixation of the steel slag can be divided into indirect carbon fixation by leaching and direct carbon fixation by thermal state. The indirect carbon fixation of the steel slag leaching is generally carried out by dissolving Ca 2+ in the steel slag by solution under the condition that the temperature is less than 200 ℃, then reacting with CO 32- in the solution to generate CaCO 3, thereby achieving the aim of indirectly fixing carbon. For example, the application of China patent application No. 202223494217.1 discloses a device for efficiently capturing carbon dioxide by activating steel slag, which is characterized in that firstly, the steel slag is crushed, then Ca 2+ is leached into solution by acid leaching, then the liquid enters a CO 2 absorption tower to absorb CO 2, however, the efficiency of indirectly fixing carbon in steel slag leaching is limited by the influence of Ca 2+ leaching rate in steel slag, and the treatment mode has large water consumption and serious environmental pollution. The thermal state direct carbon fixation is to carry out carbon fixation treatment when the steel slag is at high temperature, so that the dual purposes of steel slag carbon fixation and sensible heat utilization can be achieved, the carbon fixation efficiency of the steel slag is improved in the high temperature state, and carbonate products are also generated, so that the compactness and compressive strength of the steel slag structure are improved, the gelation activity of the steel slag is improved, the contents of f-CaO and f-MgO can be reduced, the stability of the steel slag is improved, and the recycling value of the steel slag is improved.|[0008] However, the existing steel slag carbon fixation technology ignores sensible heat recovery of steel slag, and causes a great amount of resource waste. The application number 202211142705.8 discloses a steel slag carbon fixing device and a use method thereof, wherein steel slag powder is added into a charging box, and is thrown out through a throwing tray, so that the steel slag powder reacts with CO 2 to generate carbonate for carbon fixing, and sensible heat of the steel slag is not recovered while carbon fixing. Another example is the application of chinese patent application number 202210599827.3, which discloses a method for carbon sequestration and emission reduction of wet-milled steel slag in steel works, and application thereof, wherein the application is to quench the molten steel slag produced in the steel works by water quenching, then crush, remove iron and dry the molten steel slag in sequence to obtain steel slag powder, then prepare the steel slag powder into steel slag slurry, and finally use the steel slag slurry to conduct carbon sequestration. However, the application directly quenches and quenches the molten steel slag produced by the steel plant, and the sensible heat of the steel slag is wasted.|[0009] Because the steel slag generated by the steel plant is in a molten liquid state, the temperature is higher (more than 1500 ℃), the sensible heat of the steel slag is difficult to realize by gas-liquid heat exchange, and the gas-solid heat exchange has the highest efficiency, but the complete casting of the steel slag into a solid state can cause the loss of most sensible heat of the steel slag, so that the resource waste is caused. Reducing CO2 emission, steel slag sensible heat recovery and steel slag recycling have become the problems to be solved urgently in the metallurgical industry at present.|DISCLOSURE|Disclosure of Invention|[0010] Aiming at the defects of the prior art, the invention provides a steel slag sensible heat recovery and carbon fixation modification process, so as to achieve the aim of simultaneously carrying out steel slag sensible heat recovery and steel slag carbon fixation and improving the resource utilization rate.|[0011] In order to solve the technical problems, the invention adopts the following technical scheme:|[0012] the steel slag sensible heat recovery and carbon fixation modification process comprises the following steps: |[0013] s1: the steel slag melt is cast by an ingot device, the cast high-temperature steel slag ingot shell is solid, and the inner core is liquid; |[0014] s2: the steel slag ingot enters the vertical reactor from a feed inlet at the upper part of the vertical reactor through a feeding device, metallurgical flue gas is introduced from an air inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas flows from bottom to top in the vertical reactor, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, the high-temperature steel slag ingot reacts with CO 2 in the flue gas to perform carbon fixation modification on the steel slag ingot to form a carbon fixation modified steel slag block, and the high-temperature flue gas is discharged through a pipeline at the top of the vertical reactor; |[0015] S3: the flue gas is discharged from the vertical reactor and enters a gravity dust remover for dust removal, the high-temperature flue gas after dust removal enters a heat exchanger for heat exchange, and the flue gas is discharged from a chimney after heat exchange; the carbon-fixing modified steel slag blocks are crushed and separated for grading utilization, so that the steel slag high-added-value product is prepared. |[0016] Wherein,|[0017] The temperature range of the steel slag melt is 1500-1700 ℃.|[0018] The temperature range of the cast high-temperature steel slag ingot is 900-1300 ℃.|[0019] The gas phase and the solid phase in the vertical reactor adopt countercurrent flow.|[0020] The feeding port of the vertical reactor is arranged on one side of the upper part of the vertical reactor, the air inlet pipeline is positioned on one side of the lower part, the bottom is an inverted trapezoid discharging port, and the center of the top is provided with an air outlet pipeline.|[0021] The temperature range of the flue gas discharged from the pipeline at the top of the vertical reactor is 700-1100 ℃.|[0022] The heat exchanger is a vertical heat exchanger.|[0023] The temperature of the outer shell of the high-temperature steel slag ingot is 850-900 ℃, and the temperature of the inner core of the high-temperature steel slag ingot is 1250-1300 ℃.|[0024] The two air inlet pipelines are symmetrically arranged on two sides of the lower part of the vertical reactor.|[0025] The lower part of the vertical reactor is provided with a conveying mechanism corresponding to the discharge hole, and crushing equipment and separating equipment are sequentially arranged behind the conveying mechanism.|[0026] Compared with the prior art, the invention has the following advantages:|[0027] The steel slag sensible heat recovery and carbon fixation modification process is reasonable in design, can simultaneously perform steel slag sensible heat recovery and steel slag carbon fixation, overcomes the difficulty that steel slag sensible heat recovery and steel slag carbon fixation are difficult to simultaneously perform in the prior art, improves the utilization rate of resources, reduces the running cost of enterprises, can effectively alleviate the environmental pollution problem caused by steel slag, and has important significance for the high-quality development of the metallurgical industry. |DRAWINGS DESCRIPTION|[0028] The contents and the marks in the drawings expressed in the drawings of the present specification are briefly described as follows:|[0029] FIG. 1 is a schematic diagram of the process flow of the present invention. |INVENTION MODE|Detailed Description|[0030] The following description of the embodiments of the present invention refers to the accompanying drawings, which illustrate in further detail.|[0031] The steel slag sensible heat recovery and carbon fixation modification process comprises the steps of firstly casting steel slag into blocks, wherein the cast blocks have the structural characteristics of 'wine-heart chocolate', namely, the shell is in a low-temperature solid state, the inner core is in a high-temperature liquid state, and the structure can recover the steel slag sensible heat to the greatest extent; then, the steel slag ingot is conveyed into a vertical reactor to exchange heat with metallurgical flue gas, and simultaneously the steel slag ingot reacts with carbon dioxide in the flue gas to carry out carbon fixation modification on the steel slag; and finally, recycling the steel slag after carbon fixation modification.|[0032] The process can simultaneously perform steel slag sensible heat recovery and steel slag carbon fixation, overcomes the difficulty that the steel slag sensible heat recovery and the steel slag carbon fixation are difficult to simultaneously perform in the prior art, improves the utilization rate of resources, reduces the running cost of enterprises, can effectively relieve the environmental pollution problem caused by the steel slag, and has important significance for the high-quality development of the metallurgical industry.|[0033] The preferred specific examples shown in fig. 1 are:|[0034] the slag sensible heat recovery and carbon fixation modification process based on slag ingots comprises the following steps of: |[0035] s1: the steel slag melt produced by the steel plant is cast by an ingot device, the cast high-temperature steel slag ingot has solid outer shell and liquid inner core; |[0036] S2: the high-temperature steel slag ingot enters the vertical reactor from a feed inlet at the upper part of the vertical reactor through a feeding device, metallurgical flue gas is introduced from an air inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas flows from bottom to top in the vertical reactor, the metallurgical flue gas flows reversely with the high-temperature steel slag ingot, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, the high-temperature steel slag ingot reacts with CO 2 in the flue gas to perform carbon fixation modification on the steel slag ingot, and the high-temperature flue gas is discharged through a pipeline at the top of the vertical reactor; |[0037] S3: the high-temperature flue gas is discharged from the vertical reactor and enters a gravity dust remover for dust removal, the high-temperature flue gas after dust removal enters a heat exchanger for heat exchange, and the flue gas after heat exchange is discharged from a chimney. The carbon-fixing modified steel slag blocks are crushed and separated for grading utilization, so that the steel slag high-added-value product is prepared. |[0038] Wherein,|[0039] The temperature range of the steel slag melt is 1500-1700 ℃; the temperature range of the cast high-temperature steel slag ingot is 900-1300 ℃, and the shape of the cast high-temperature steel slag ingot can be square, cuboid, arc-shaped side and cylinder, the outer shell temperature is 850-900 ℃, and the inner core temperature is 1250-1300 ℃.|[0040] The feeding port at the upper part of the vertical reactor is arranged at one side of the vertical reactor, the lower part is provided with two air inlet pipelines which are respectively symmetrically arranged at the left side and the right side, the bottom is inverted trapezoid and is provided with a discharging port, and the center of the top is provided with an air outlet pipeline; the temperature range of the flue gas discharged from the pipeline at the top of the vertical reactor is 700-1100 ℃.|[0041] The heat exchanger is a vertical heat exchanger; the vertical reactor, the gravity dust remover, the heat exchanger and the chimney are all connected by pipelines. The lower part of the vertical reactor is provided with a conveying mechanism corresponding to the discharge hole, and crushing equipment and separating equipment are sequentially arranged behind the conveying mechanism, wherein the crushing equipment and the separating equipment can adopt the existing equipment.|[0042] Because the steel slag generated by the steel plant is in a molten liquid state, the temperature is higher (more than 1500 ℃), the sensible heat of the steel slag is difficult to realize by gas-liquid heat exchange, and the gas-solid heat exchange has the highest efficiency, but the complete casting of the steel slag into a solid state can cause the loss of most sensible heat of the steel slag, so that the resource waste is caused. Aiming at the problem, the applicant creatively provides a high-temperature steel slag ingot with the structural characteristic of the chocolate with wine centers, and the steel slag ingot has the outer shell in a low-temperature solid state and the inner core in a high-temperature liquid state.|[0043] The applicant carries out systematic research on the carbon fixation characteristics of steel slag and metallurgical flue gas of a steel plant, and discovers that the reaction temperature has great influence on the direct carbon fixation of the steel slag. The carbon fixation reaction does not substantially occur at 500 ℃, and when the temperature is 650 ℃ or higher, the obvious carbon fixation reaction occurs, but at 950 ℃ the concentration of CO 2 starts to rise with the extension of time, which indicates that the carbonate is decomposed again. In order to solve the problem, the applicant proposes a structural design of the vertical reactor, wherein the design adopts gas-solid countercurrent, so that the carbon-fixing reaction fully occurs in a low-temperature region, the decomposition of carbonate in a high-temperature region is avoided, and the high-temperature steel slag ingot is fully reacted in the vertical reactor.|[0044] The invention carries out the industrial experiments of sensible heat recovery and carbon fixation of the converter steel slag; the specific embodiment is as follows:|[0045] The temperature of the converter steel slag melt is 1550 ℃, the temperature of the cast high-temperature steel slag ingot shell is 870 ℃, the temperature of the cast high-temperature steel slag ingot inner core is 1280 ℃, the residence time of the steel slag ingot in the vertical reactor is 1.8h, the temperature of the carbon-fixing modified steel slag is 58 ℃ after carbon fixing and heat exchange, the carbon-fixing conversion rate is up to 92%, the temperature of high-temperature flue gas input by the vertical reactor is 960 ℃, and the sensible heat recovery rate of the steel slag is up to 75%; the method can simultaneously recover the sensible heat of the steel slag and fix the carbon of the steel slag, and overcomes the difficulty that the sensible heat recovery of the steel slag and the carbon fixation of the steel slag are difficult to simultaneously carry out in the prior art. |[0046] The invention has the following advantages:|[0047] 1. By casting the molten steel slag, the shell of the casting is in a low-temperature solid state, and the shell is in a high-temperature liquid state, so that the structure can realize solid conveying of slag, liquid heat exchange of solid steel slag and greatly improve the sensible heat recovery rate of steel slag; 2. the structural design of the vertical reactor is provided, and the gas phase and the solid phase in the vertical reactor flow reversely, so that the carbon fixation reaction fully occurs in a low temperature area, the decomposition of carbonate in a high temperature area is avoided, and the direct carbon fixation efficiency of the steel slag is greatly improved; 3. the ultimate recovery of the sensible heat of slag can be realized, the direct solidification of metallurgical flue gas CO 2 can be realized, the steel slag can be modified through carbonation, and the modified steel slag can be used for high added value. |[0048] While the invention has been described above with reference to the accompanying drawings, it will be apparent that the invention is not limited to the above embodiments, but is capable of being modified or applied to other applications without any modification, as long as the inventive concept and technical scheme are adopted. Family Number|(110341563)|110341563|Abstract|(CN118239702 A)|The invention discloses a steel slag sensible heat recovery and carbon sequestration modification process , which comprises the following steps that a steel slag melt is subjected to ingot casting through an ingot casting device , a cast high - temperature steel slag ingot shell is in a solid state , and an inner core is in a liquid state ; the steel slag ingot enters the vertical reactor from a feeding hole in the upper part of the vertical reactor , meanwhile , metallurgical flue gas is introduced from a gas inlet pipeline at the bottom of the vertical reactor , the metallurgical flue gas exchanges heat with the high - temperature steel slag ingot in the flowing process to form high - temperature flue gas , and meanwhile , the high - temperature steel slag ingot reacts with CO2 in the flue gas to form CO2 in the high - temperature flue gas ; carrying out carbon sequestration modification on the steel slag ingot to form a carbon sequestration modified steel slag block , and discharging high - temperature flue gas through a pipeline at the top of the vertical reactor ; s3 , the dedusted high - temperature flue gas enters a heat exchanger for heat exchange , and the flue gas is discharged from a chimney after heat exchange ; the carbon sequestration modified steel slag blocks are crushed , separated and then graded for utilization , and high - added - value steel slag products are prepared . And steel slag sensible heat recovery and steel slag carbon sequestration can be performed simultaneously . |CPC codes|(CN118239702 A)|B01D - 053/62 |B01D - 053/82 |B01D - 2257/504 |B01D - 2258/0283 |IPC codes|(CN118239702 A)|B01D - 053/62 |B01D - 053/82 |Title|(CN118239702 A)|Steel slag sensible heat recovery and carbon sequestration modification process | Environmental technology|Materials, metallurgy|Thermal processes and apparatus B01D-053/62|B01D-053/82|B01D-2257/504|B01D-2258/0283|C04B-005/06|C04B-007/147|C04B-018/14/2|C04B-020/02/3|F27D-017/10|F27D-017/30 B01D-053/62|B01D-053/82|B01D-2257/504|B01D-2258/0283|C04B-005/06|C04B-007/147|C04B-018/14/2|C04B-020/02/3|F27D-017/10|F27D-017/30 B01D-053/62|B01D-053/82|C04B-005/06|C04B-007/147|C04B-018/14|C04B-020/02|F27D-017/00 B01D-053/62|B01D-053/82|C04B-005/06|C04B-007/147|C04B-018/14|C04B-020/02|F27D-017/00 PENDING (CN118239702)|PENDING ALIVE (CN118239702)|ALIVE (CN118239702)|LEGAL DETAILS FOR CN118239702|Actual or expected expiration date=2044-03-11|Legal state=ALIVE|Status=PENDING|Event publication date=2024-03-11|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202410273042|Application date=2024-03-11|Standardized application number=2024CN-0273042|Event publication date=2024-06-25|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN118239702|Publication stage code=A|Publication date=2024-06-25|Standardized publication number=CN118239702|Event publication date=2024-06-25|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-07-12|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN118239702)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoS5CWsC5calelfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073272575&ekey=2349&xpn=CN118239702&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=VhJ8aA%252FSbkar0961cXayjJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN118239702)|CN (CN118239702)|NAME=ANHUI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN118239702)|NAME=ZHANG YONGSHENG;ANHUI INTELLECTUAL PROPERTY AGENCY CO LTD , REG=34107 (CN118239702)|NAME=LONG HONGMING|NAME=WEI RUFEI|NAME=FAN CHUNLONG|NAME=SUN RONG|NAME=ZHANG HAO|NAME=DI ZHANXIA 0 1 Titre: (CN118239702)|Steel slag sensible heat recovery and carbon sequestration modification process Résumé: (CN118239702)|The invention discloses a steel slag sensible heat recovery and carbon sequestration modification process, which comprises the following steps that a steel slag melt is subjected to ingot casting through an ingot casting device, a cast high-temperature steel slag ingot shell is in a solid state, and an inner core is in a liquid state; the steel slag ingot enters the vertical reactor from a feeding hole in the upper part of the vertical reactor, meanwhile, metallurgical flue gas is introduced from a gas inlet pipeline at the bottom of the vertical reactor, the metallurgical flue gas exchanges heat with the high-temperature steel slag ingot in the flowing process to form high-temperature flue gas, and meanwhile, the high-temperature steel slag ingot reacts with CO2 in the flue gas to form CO2 in the high-temperature flue gas; carrying out carbon sequestration modification on the steel slag ingot to form a carbon sequestration modified steel slag block, and discharging high-temperature flue gas through a pipeline at the top of the vertical reactor; s3, the dedusted high-temperature flue gas enters a heat exchanger for heat exchange, and the flue gas is discharged from a chimney after heat exchange; the carbon sequestration modified steel slag blocks are crushed, separated and then graded for utilization, and high-added-value steel slag products are prepared. And steel slag sensible heat recovery and steel slag carbon sequestration can be performed simultaneously. 37 Abstract gpt-4o-mini no The focus is on steel slag processing and heat recovery rather than on accelerating the chemical weathering of minerals for CO₂ capture.
38 CN202211087853 CN202211087853 CN115591395|CN115591395 103441127 CN115591395 B 2025-08-08 [CN115591395B]|CN115591395 A 2023-01-13 [CN115591395] 2022-09-07 2022-09-07 2025-08-08|2023-01-13 (CN115591395B)|2025-08-08 (CN115591395)|2042-09-07 (CN115591395)|Method for strengthening carbon fixation of feldspar mineral by composite microorganisms (CN115591395)|The invention discloses a method for enhancing carbon sequestration of feldspar minerals by compound microorganisms, which comprises the following steps: crushing feldspar minerals, pulping, pumping into a carbon sequestration bioreactor containing aspergillus and silicate bacteria, and absorbing slurry in an upflow state in a flow guide inner cylinder of the reactor, then downwards reflowing to the bottom of the reactor along a space between the outer side of the flow guide inner cylinder and the inner wall of the reactor; cO2 is blown in from the bottom of the reactor and is in full contact with a biological membrane and suspended microorganisms, the CO2 is dissolved in absorption slurry and reacts with metal cations dissolved out of feldspar minerals, finally, the CO2 is converted into indissolvable carbonate precipitates, and the purpose of carbon sequestration is achieved. According to the method, the feldspar mineral is used as the raw material for pulping and fixing CO2, the raw material source is wide, the absorption rate is high, and the carbon fixation process is obvious; products such as small molecular acid are generated by metabolism of the compound microorganisms, decomposition of feldspar minerals is accelerated, metal cations are released into absorption slurry, potassium in the feldspar minerals is converted into a soluble state, subsequent potassium extraction is facilitated, and the dual effects of carbon sequestration and potassium release are achieved. KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY (CN115591395)|KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN])|(CN115591395)|KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) LIU SHUGEN|YE FUYING|WANG QIONGHUI|PENG YUXIN|TIAN SENLIN|NING PING|SHI JIANWU (CN115591395)|LIU SHUGEN|YE FUYING|WANG QIONGHUI|PENG YUXIN|TIAN SENLIN|NING PING|SHI JIANWU|(CN115591395)|LIU SHUGEN|YE FUYING|WANG QIONGHUI|PENG YUXIN|TIAN SENLIN|NING PING|SHI JIANWU (CN115591395)|ZHANG YANG;Kunming Tongju Patent Agency Co., Ltd.|Reg. Nb: 53214|ZHANG YU;Kunming Tongju Patent Agency Co., Ltd.|Reg. Nb: 53214 (CN115591395)|1. The method for solidifying carbon by using the composite microorganism reinforced feldspar mineral is characterized by comprising the following steps of: S1, loading aspergillus aculeatus into a velvet-shaped filler, fixing the filler to a fixed frame of a guide inner cylinder of a carbon-fixing bioreactor, and simultaneously adding the silicate bacteria after multiplication culture into the reactor, wherein the feldspar minerals are crushed to a particle size of less than 100 mu m and then uniformly mixed with an absorption liquid to prepare an absorption slurry, and then pumping the absorption slurry into the reactor containing the aspergillus aculeatus and the silicate bacteria, wherein the culture process of the silicate bacteria is to rinse root system soil in a cotton bud period by using 0.5% citric acid, add potassium feldspar mineral powder according to the mass of the rinse solution, culture for 7 days under the condition of pH7.5, and perform centrifugal treatment to collect wet-based thalli, wherein the silicate bacteria are added into the reactor according to the proportion of 0.6-1.5% of the total mass of the absorption liquid; S2, CO 2 is sent into the reactor through an aeration device at the bottom of the carbon-fixing bioreactor, fully contacts with absorption slurry in the guide inner cylinder and is in an ascending flow state, and fully contacts with biological membranes and suspended microorganisms, then the absorption slurry flows downwards to the bottom of the reactor in a space between the outer side of the guide inner cylinder and the inner side of the reactor and is discharged, the discharged absorption slurry is conveyed by a conveying pump, is sprayed out from a spiral spray head at the inner top of the reactor and is in countercurrent contact with CO 2 escaped from a liquid-phase absorption system in the reactor, and CO 2 is finally converted into carbonate sediment and is discharged. | (CN115591395)|The invention aims to provide a method for strengthening carbon fixation of feldspar minerals by composite microorganisms, which comprises the steps of pulping the feldspar minerals, adding the pulped feldspar minerals into a carbon fixation bioreactor, constructing a composite microorganism system with coexistent suspension and adhesion growth states, bubbling CO _2 from the bottom of the reactor and fully contacting with a biological membrane and suspended microorganisms, dissolving out metal cations such as calcium and iron dissolved in the feldspar minerals and reacting with CO _2, and finally converting the dissolved metal cations into insoluble carbonate for precipitation so as to achieve the aim of carbon fixation, wherein after aspergillus aculeatus and silicate bacteria are added into the reactor, the content of metabolites such as small molecular acid in an absorption liquid is higher, accelerating the decomposition of the feldspar minerals and releasing metal cations such as potassium into the absorption liquid, thereby improving the effect of carbon fixation and potassium release.The object of the invention is achieved in that it comprises the following steps:|The invention discloses a method for solidifying carbon by a composite microorganism reinforced feldspar mineral, which comprises the steps of pulping after crushing the feldspar mineral, pumping the crushed feldspar mineral into a carbon solidifying bioreactor containing aspergillus and silicate bacteria, enabling absorption slurry to be in an ascending flow state in the inner guide cylinder of the reactor, then enabling the absorption slurry to flow back to the bottom of the reactor downwards along a space between the outer side of the inner guide cylinder and the inner wall of the reactor, bubbling CO 2 from the bottom of the reactor and fully contacting with a biomembrane and suspended microorganisms, dissolving CO 2 in the absorption slurry and acting with metal cations dissolved in the feldspar mineral, and finally converting the absorption slurry into insoluble carbonate precipitate, thereby achieving the purpose of solidifying carbon.| (CN115591395)|FELDSPAR MINERAL(100,32)|COMPOSITE MICROORGANISM(100,11)|SOLIDIFYING CARBON(100,5)|STRENGTHENING CARBON FIXATION(100,2)|SILICATE BACTERIUM(67,12)|ABSORPTION SLURRY(60,41)|PULPED FELDSPAR MINERAL(47,1)|MICROORGANISM SUSPENSION(46,4)|CARBON SOLIDIFYING BIOREACTOR(43,2)|REINFORCED FELDSPAR MINERAL(39,2)|CRUSHED FELDSPAR(39,1)|INSOLUBLE CARBONATE PRECIPITATE(38,1)|REACTOR(32,56)|COMPOSITE MICROORGANISM METABOLISM(32,1)|WET THALLUS(31,1)|POTASSIUM FELDSPAR(29,5)|CARBONATE PRECIPITATE(28,1)|COEXISTENT SUSPENSION(27,1)|DISCHARGED ABSORPTION SLURRY(26,2)|LOADING ASPERGILLUS ACULEATUS(26,2)|MULTIPLICATION CULTURE(26,2)|SPIRAL SPRAY HEAD(25,7)|CARBONATE SEDIMENT(24,2)|COMPOSITE MICROORGANISM CARBON FIXATION(24,2)|GUIDE INNER CYLINDER(23,28)|CARBON FIXING BIOREACTOR(22,6)|ABSORPTION SLURRY DOSAGE(22,1)|CENTRIFUGAL TREATMENT(22,1)|INNER GUIDE CYLINDER(21,2)|ADHESION GROWTH(21,1)|CARBON FIXATION BIOREACTOR(21,1)|INSOLUBLE CARBONATE(21,1)|ASPERGILLUS ACULEATUS(20,6)|BUBBLING(20,2)|FELDSPAR(19,8)|METAL CATION(19,7)|COMPOSITE MICROORGANISM CARBON SEQUESTRATION(19,1)|RINSE SOLUTION(19,1)|EMPTYING PIPE(18,6)|DECOMPOSITION(18,2)|QUANTITATIVE ABSORPTION SLURRY ACCOUNT(18,2)|ASPERGILLUS(18,1)|REACTOR INNER GUIDE CYLINDER(18,1)|ABSORPTION LIQUID(17,16)|CULTURE(17,3)|COTTON BUD MENSTRUATION(17,1)|CARBON DIOXIDE AERATION(16,11)|POTASSIUM RELEASE(16,1)|CARBON FIXATION(15,10)|BIOLOGICAL MEMBRANE(15,3)|BIOMEMBRANE(15,2)|POTASSIUM EXTRACTION(15,2)|CONVEYING PUMP(14,7)|DISSOLVED METAL CATION(14,1)|VELVET SHAPED FILLER(13,8)|PULPING TANK BOTTOM(13,7)|AERATION(13,3)|WASTE SLURRY DISCHARGE(13,2)|PRECIPITATION(13,1)|TEMPORARY FEEDING PORT(12,5)|ASPERGILLUS ACULEATUS SPORE SUSPENSION(12,4)|COUNTERCURRENT(12,4)|PULPING GROOVE BOTTOM(11,1)|FIXED FRAME(10,15)|MINERAL(10,2)|FILLER(9,9)|WASTE ABSORPTION LIQUID(9,4)|TOTAL ABSORPTION SLURRY(9,2)|ASCENDING FLOW STATE(8,3)|ABSORPTION RATE(8,2)|AIR PIPELINE(8,2)|OXYGEN CONTENT(8,2)|SOLID CONTENT(7,6)|ANORTHITE(7,4)|BIOTITE(7,3)|ABSORPTION SLURRY EQUAL VOLUME(7,2)|ROOT SYSTEM GROUND(7,1)|ABSORPTION LIQUOR(6,4)|TAIL GAS DISCHARGE(6,4)|ABSORBING LIQUID PHASE(6,3)|ADDING POTASSIUM FELDSPAR(6,3)|CONVEYING PIPE INNER WALL(6,1)|FELDSPAR MINERAL DECOMPOSITION(6,1)|PROLIFERATED WET SILICATE BACTERIUM(6,1)|PH VALUE(5,4)|AIR INLET(5,3)|FELDSPAR MIXED MINERAL(5,2)|MUNICIPAL DOMESTIC SEWAGE(5,2)|URBAN DOMESTIC SEWAGE(5,2)|ASPERGILLUS ACULEATUS INOCULATION(5,1)|CITRIC ACID(4,7)|LIQUID CIRCULATION(4,7)|INNER WALL(4,5)|DIVERSION INNER CYLINDER(4,3)|SMALL MOLECULAR ACID(4,3)|PARTICLE SIZE(4,2)|COMPOUND MICROORGANISM METABOLISM(4,1)|FEEDING WET BACTERIUM(4,1)|MIX PRETREATED POTASSIUM(4,1)|WET BACTERIUM CONSUMPTION(4,1)|OUTER SIDE(3,4)|REACTOR GUIDE INNER CYLINDER(3,4)|RETURN PIPE(3,4)|CYLINDRICAL STRUCTURE(3,3)|POTASSIUM ADDITION(3,3)|CITRIC ACID ORGANIC WASTEWATER(3,2)|REACTION ABSORPTION(3,2)|ALGAE ABSORPTION(3,1)|CARBON SEQUESTRATION BIOREACTOR(3,1)|DISSOLVABLE CARBONATE(3,1)|EVACUATION PIPE(3,1)|FLOWING ABSORPTION SLURRY(3,1)|PROLIFERATION CULTURE(3,1)|RESOURCE UTILIZATION(3,1)|SILICATE SUBSTANCE(3,1)|TAIL GAS PURIFICATION(3,1)|TANK CIRCULATION(3,1)|WASTE ABSORPTION SLURRY(3,1)|CARBON FIXING(2,2)||(CN115591395)|FELDSPAR MINERAL(100,42)|CARBON FIXATION(100,19)|COMPOSITE MICROORGANISM(100,14)|FELDSPAR MINERAL CARBON FIXATION(100,5)|SILICATE BACTERIUM(46,11)|STRENGTHENING CARBON SEQUESTRATION(42,9)|ABSORPTION SLURRY(41,37)|INSOLUBLE CARBONATE PRECIPITATE(41,2)|MICROORGANISM SUSPENSION(40,4)|CARBON FIXATION BIOREACTOR(37,3)|FELDSPAR MINERAL DECOMPOSITION(37,1)|CARBONATE PRECIPITATE(35,4)|PULPING TANK(32,26)|REACTOR(31,55)|PULPED FELDSPAR(29,1)|DISCHARGED ABSORPTION SLURRY(28,1)|DIVERSION INNER CYLINDER(23,10)|COTTON LEACHING ROOT SOIL(23,2)|LOADING ASPERGILLUS ACULEATUS(22,2)|CO EXISTING SUSPENSION(22,1)|SPIRAL SPRAY HEAD(20,4)|EVACUATION PIPE(20,2)|ASPERGILLUS SPORE SUSPENSION(19,5)|PROLIFERATION CULTURE(19,4)|REINFORCING CARBON FIXATION(19,1)|METAL CATION(18,6)|ABSORPTION PULP(18,2)|POTASSIUM RELEASE(18,2)|ADHESION GROWTH(18,1)|COMPOSITE MICROORGANISM AID(18,1)|ABSORPTION LIQUID(17,20)|ASPERGILLUS ACULEATUS(17,6)|BIOLOGICAL MEMBRANE(17,4)|ASPERGILLUS(17,2)|INNER CYLINDER(16,15)|CONVEYING PUMP(16,6)|VELVET SHAPED FILLER(16,4)|ADDING POTASH FELDSPAR(16,2)|QUANTITATIVE ABSORPTION SLURRY ACCOUNT(16,2)|ADDING SILICATE BACTERIUM(16,1)|FLUFFY FILLER(16,1)|POTASSIUM EXTRACTION(16,1)|SPIRAL NOZZLE(15,5)|CARBON FIXING BIOREACTOR(15,2)|RAW MATERIALTHE ABSORPTION RATE(15,1)|WET BACTERIUM(15,1)|FIXED FRAME(14,14)|CARBON DIOXIDE AERATION(14,10)|PULPING TANK BOTTOM(14,10)|CONVEYING PIPE(14,6)|URBAN DOMESTIC SEWAGE(14,5)|BIOFILM CULTURING MODE(14,2)|BUBBLING(14,1)|VELVET FILLER(13,3)|AERATION(12,3)|LEACHEATE MASS(12,2)|MICROMOLECULAR ACID(12,2)|WASTEWATER(12,2)|CARBON SEQUESTRATION BIOREACTOR(11,5)|REACTOR FIXING FRAME(11,2)|WASTE SLURRY DISCHARGE(11,2)|GUIDE INNER CYLINDER(10,5)|CO2(10,4)|COUNTERCURRENT CONTACT(10,3)|TEMPORARY FEEDING PORT(10,3)|CENTRIFUGAL TREATMENT(9,2)|ASPERGILLUS ACULEATUS CULTURE(9,1)|BLOWING(9,1)|INOCULATION(8,4)|WASTE ABSORPTION LIQUID(8,4)|TOTAL ABSORPTION SLURRY MASS(8,1)|ASCENDING FLOW STATE(7,3)|ASPERGILLUS ACULEATUS SPORE SUSPENSION(7,2)|BUD(7,2)|OXYGEN CONTENT(7,2)|METABOLIC PRODUCT(7,1)|ANORTHITE(6,5)|BIOTITE(6,4)|ABSORPTION SLURRY EQUAL VOLUME(6,2)|EMPTYING PIPE(5,4)|FLOW GUIDE INNER CYLINDER(5,4)|TAIL GAS DISCHARGE(5,4)|ABSORBING LIQUID PHASE(5,3)|GAS INLET(5,2)|WET SILICATE BACTERIUM DOSAGE(5,1)|LIQUID CIRCULATION(4,10)|PH VALUE(4,4)|SOLID CONTENT(4,3)|SOLID CULTURE MEDIUM(4,3)|ADDING POTASSIUM FELDSPAR(4,2)|COMPOUND MICROORGANISM METABOLISM(4,1)|DISCHARGEDTHE DISCHARGED ABSORPTION SLURRY(4,1)|EXOGENOUS MEDICAMENT(4,1)|PRETREATED FELDSPAR POTASSIUM POWDER(4,1)|SILICATE BACTERIUM CHOKE(4,1)|WIDE SOURCE(4,1)|OUTER SIDE(3,4)|GAS PIPELINE(3,3)|INNER WALL(3,3)|LIQUID CULTURE SOLUTION(3,3)|REACTOR DIVERSION INNER CYLINDER(3,3)|CYLINDRICAL TUBULAR STRUCTURE(3,2)|PARTICLE SIZE(3,2)|ABSORPTION SLURRY CIRCULATION(3,1)|FELDSPAR MIXED MINERAL(3,1)|LITHIUM ZIRCONATE(3,1)|ORGANIC WASTEWATER ACCOUNT(3,1)|POTASSIUM EXTRACTION UTILIZATION(3,1)|SLAG CALCINATION(3,1)|SMALL MOLECULAR ACID(3,1)|WASTE ABSORPTION SLURRY(3,1)|ACETIC ACID(2,4)|RETURN PIPE(2,4)|BIOFILM(2,3)|CARBON FIXATION(2,3)|ZIRCONIUM NITRATE(2,3)|ADDED MICROORGANISM(2,2)|CITRIC ACID ORGANIC WASTEWATER(2,2)|DOMESTIC SEWAGE(2,2)|MASS PERCENT(2,2)|POTASSIUM ADDITION(2,2)|ALGAE ABSORPTION(2,1)|INSOLUBLE CARBONATE(2,1)|MINERALIZATION CARBON FIXATION(2,1)|RESOURCE UTILIZATION(2,1)|SILICATE SUBSTANCE(2,1)|TAIL GAS PURIFICATION(2,1)|TANK CIRCULATION(2,1)| (CN115591395)|1. The method for solidifying carbon by using the composite microorganism reinforced feldspar mineral is characterized by comprising the following steps of:| S1, loading aspergillus aculeatus into a velvet-shaped filler, fixing the filler to a fixed frame of a guide inner cylinder of a carbon-fixing bioreactor, and simultaneously adding the silicate bacteria after multiplication culture into the reactor, wherein the feldspar minerals are crushed to a particle size of less than 100 mu m and then uniformly mixed with an absorption liquid to prepare an absorption slurry, and then pumping the absorption slurry into the reactor containing the aspergillus aculeatus and the silicate bacteria, wherein the culture process of the silicate bacteria is to rinse root system soil in a cotton bud period by using 0.5% citric acid, add potassium feldspar mineral powder according to the mass of the rinse solution, culture for 7 days under the condition of pH7.5, and perform centrifugal treatment to collect wet-based thalli, wherein the silicate bacteria are added into the reactor according to the proportion of 0.6-1.5% of the total mass of the absorption liquid; | S2, CO 2 is sent into the reactor through an aeration device at the bottom of the carbon-fixing bioreactor, fully contacts with absorption slurry in the guide inner cylinder and is in an ascending flow state, and fully contacts with biological membranes and suspended microorganisms, then the absorption slurry flows downwards to the bottom of the reactor in a space between the outer side of the guide inner cylinder and the inner side of the reactor and is discharged, the discharged absorption slurry is conveyed by a conveying pump, is sprayed out from a spiral spray head at the inner top of the reactor and is in countercurrent contact with CO 2 escaped from a liquid-phase absorption system in the reactor, and CO 2 is finally converted into carbonate sediment and is discharged. |2. The method for carbon fixation of a composite microbial reinforced feldspar mineral according to claim 1, wherein the feldspar mineral is one or more of potassium feldspar, anorthite or biotite, and the solid content of the feldspar mineral in the absorption slurry is 1.5-4.5%, wherein the mass percentage is.|3. The method for carbon sequestration of the composite microorganism reinforced feldspar minerals according to claim 1, wherein the concentration of CO 2 introduced into the reactor is 0.5-15%, the oxygen content is not less than 15%, and the residence time of the gas in the absorption system is 5-15 s.|4. The method for carbon fixation of composite microorganism reinforced feldspar minerals according to claim 1, wherein the pH value of the absorption slurry in the reactor is controlled to 7.2-9.5, when the pH value is lower than 7.2, quantitative absorption slurry is discharged from the bottom of the pulping tank, then an equal volume of fresh absorption slurry is supplemented, and meanwhile feldspar minerals are added, wherein the dosage of the absorption slurry is 0.8-1.2 times of the solid content in the waste absorption liquid.|5. The method for carbon sequestration of composite microbial reinforced feldspar minerals according to claim 4, wherein the quantitative absorption slurry accounts for 10-20% of the total absorption slurry by mass.|6. The method for solidifying carbon by using the composite microorganism reinforced feldspar mineral according to claim 1, wherein the carbon-solidifying bioreactor comprises a reactor body (1), a spiral spray head (2), a guide inner cylinder (3), a fixed frame body (4), a carbon dioxide aeration device (5) and an emptying pipe (6), wherein the spiral spray head (2) is arranged at the top in the reactor body (1), the reactor body (1) is internally provided with the guide inner cylinder (3), the guide inner cylinder (3) is in a cylindrical structure, the inside of the guide inner cylinder is hollow, the upper end and the lower end of the guide inner cylinder are open, a space is reserved between the guide inner cylinder (3) and the inner wall of the reactor body (1), the fixed frame body (4) is arranged in the guide inner cylinder (3), the carbon dioxide aeration device (5) is arranged at the bottom in the reactor body (1), the bottom of the reactor body (1) is provided with the emptying pipe (6), the fixed frame body (4) is internally provided with a velvet-shaped filler (7), the bottom of the reactor body (1) is communicated with the bottom of a pulping tank (9) through a return pipe (8), the pulping tank (9) is communicated with the inner wall of the conveying pipe (2) through the conveying pipe (2), the conveying pipe (10) is provided with a stirring device (11), the bottom of the pulping groove (9) is provided with a waste slurry discharge port (12).|7. The method for carbon fixation of the composite microorganism reinforced feldspar mineral according to claim 6, wherein the upper part of the side surface of the reactor body (1) is provided with an observation and temporary feeding port (13), the top of the reactor body (1) is provided with a tail gas discharge port (14), and the carbon dioxide aeration device (5) is communicated with an air inlet buffer tank (15) through an air pipeline. (CN115591395)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of industrial tail gas purification and resource utilization, and particularly relates to a method for solidifying carbon by a composite microorganism reinforced feldspar mineral.|BACKGROUND ART|[0002] With the increasing demand of human society for fossil fuels, the carbon dioxide emission in industrial production process is rapidly increased, and the problem of greenhouse effect caused by carbon dioxide is widely focused. The main methods of capturing, sealing or fixing carbon dioxide commonly used at present are plant or algae absorption and conversion, physical adsorption, air separation/exhaust circulation method, chemical absorption method and the like. The chemical absorption method separates carbon dioxide from the mixed gas by utilizing chemical reaction between the carbon dioxide and the absorption slurry, and has the characteristics of large absorption capacity, good absorption effect, lower cost and the like, so that the method is more focused in practical application.|[0003] The prior patent CN109261116A uses zirconium oxynitrate as a zirconium source, lithium hydroxide as a lithium source, carbonate as a precipitator, and carries out precipitation reaction in ammonia water solution, filtering or evaporating to remove water after the reaction, and then drying and roasting to obtain the lithium zirconate adsorption material. The prior patent CN107902631A uniformly mixes pretreated potassium feldspar powder, carbon powder and calcium sulfate, tabletting and forming, and collecting sulfur dioxide after high-temperature activation reaction under nitrogen atmosphere, mineralizing and calcining slag by adopting CO2, and separating and obtaining mineralized slag containing calcium carbonate and water-soluble potassium sulfate fertilizer. However, the method needs to add a large amount of exogenous agents, and the operation cost of the mineralized carbon fixation process is obviously increased. In natural environment, silicate substances and metal cations such as calcium, iron and the like are generated after the feldspar minerals are decomposed, and dissolved metal cations react with carbon dioxide to generate indissolvable carbonate, but the progress of carbon fixation through the above approaches is very slow. The development of efficient and cost-effective carbon sequestration technology has significant implications for implementation of new-period two-carbon action plans.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a method for strengthening carbon fixation of feldspar minerals by composite microorganisms, which comprises the steps of pulping the feldspar minerals, adding the pulped feldspar minerals into a carbon fixation bioreactor, constructing a composite microorganism system with coexistent suspension and adhesion growth states, bubbling CO 2 from the bottom of the reactor and fully contacting with a biological membrane and suspended microorganisms, dissolving out metal cations such as calcium and iron dissolved in the feldspar minerals and reacting with CO 2, and finally converting the dissolved metal cations into insoluble carbonate for precipitation so as to achieve the aim of carbon fixation, wherein after aspergillus aculeatus and silicate bacteria are added into the reactor, the content of metabolites such as small molecular acid in an absorption liquid is higher, accelerating the decomposition of the feldspar minerals and releasing metal cations such as potassium into the absorption liquid, thereby improving the effect of carbon fixation and potassium release.|[0005] The object of the invention is achieved in that it comprises the following steps:|[0006] s1, loading aspergillus aculeatus into a velvet-shaped filler, fixing the filler to a fixed frame body of a guide inner cylinder of a carbon-fixing bioreactor, and simultaneously adding silicate bacteria after multiplication culture into the reactor, wherein feldspar minerals are crushed to a particle size of less than 100 mu m, then uniformly mixed with an absorption liquid in a pulping tank to prepare absorption slurry, and then pumped into the reactor containing aspergillus aculeatus and silicate bacteria; |[0007] S2, CO 2 is sent into the reactor through an aeration device at the bottom of the carbon-fixing bioreactor, fully contacts with absorption slurry in the guide inner cylinder and is in an ascending flow state, and fully contacts with biological membranes and suspended microorganisms, then the absorption slurry flows downwards to the bottom of the reactor in a space between the outer side of the guide inner cylinder and the inner side of the reactor and is discharged, the discharged absorption slurry is conveyed by a conveying pump, is sprayed out from a spiral spray head at the inner top of the reactor and is in countercurrent contact with CO 2 escaped from a liquid-phase absorption system in the reactor, and CO 2 is finally converted into carbonate sediment and is discharged. |[0008] Preferably, the silicate bacteria are cultured by leaching root system soil in a bud stage by using 0.5% of citric acid, adding potassium feldspar mineral powder according to the mass of leaching solution of 0.5%, culturing for 7 days under the condition of pH of 7.5, centrifuging to collect wet-base bacteria, and adding the silicate bacteria into a reactor according to the proportion of 0.6-1.5% of the total mass of absorption liquid.|[0009] Preferably, the aspergillus aculeatus is inoculated into a solid culture medium to prepare an aspergillus aculeatus spore suspension, then the aspergillus aculeatus is inoculated into a liquid culture solution filled with velvet-shaped fillers, the inoculation concentration is 0.1-1 multiplied by 10 6/mL, the membrane is hung for 3 days for culture, then the fillers are taken out, the fillers are fixed to a fixed frame body of a guide inner cylinder of a reactor after being taken out, and the mass ratio of the fillers to an absorption liquid is 25-40:100.|[0010] Preferably, the feldspar mineral is one or more of potassium feldspar, anorthite or biotite, and the solid content of the feldspar mineral in the absorption slurry is 1.5-4.5%, wherein the percentage is the mass percentage.|[0011] Preferably, the absorption liquid is prepared from urban domestic sewage and organic wastewater containing citric acid and acetic acid, and the chemical oxygen demand of the absorption liquid is controlled to be 350-500 mg/L.|[0012] Preferably, the concentration of CO 2 fed into the reactor is 0.5-15% (volume percent), the oxygen content is not less than 15% (volume percent), and the residence time of the gas in the absorption system is 5-15 s.|[0013] Preferably, the pH value of the absorption slurry in the reactor is controlled to be 7.2-9.5, when the pH value is lower than 7.2, quantitative absorption slurry is discharged from the bottom of the pulping tank, then the equal volume of fresh absorption slurry is supplemented, and meanwhile feldspar minerals are added, wherein the dosage of the feldspar minerals is 0.8-1.2 times of the solid content in the waste absorption liquid.|[0014] Preferably, the quantitative absorption slurry accounts for 10-20% of the total absorption slurry by mass.|[0015] Preferably, the carbon-fixing bioreactor comprises a reactor body, a spiral spray head, a guide inner cylinder, a fixed frame body, a carbon dioxide aeration device and an emptying pipe, wherein the spiral spray head is arranged at the top of the reactor body, the guide inner cylinder is arranged in the reactor body and is of a cylindrical structure, the inside of the reactor body is hollow, the upper end and the lower end of the reactor body are open, a space is reserved between the guide inner cylinder and the inner wall of the reactor body, the fixed frame body is arranged in the guide inner cylinder, the carbon dioxide aeration device is arranged at the bottom of the reactor body, the emptying pipe is arranged at the bottom of the reactor body, a velvet-shaped filler is filled in the fixed frame body, the bottom of the reactor body is communicated with the bottom of a pulping tank through a return pipe, the pulping tank is communicated with the spiral spray head through a conveying pipe, a conveying pump is arranged in the conveying pump, and a stirring device is arranged in the pulping tank, and the bottom of the pulping tank is provided with a waste slurry discharge port.|[0016] Preferably, the upper part of the side surface of the reactor body is provided with an observation and temporary feeding port, the top of the reactor body is provided with a tail gas discharge port, and the carbon dioxide aeration device is communicated with the air inlet buffer tank through a gas pipeline.|[0017] Compared with the prior art, the invention has the following technical effects:|[0018] 1. The method takes feldspar minerals as raw materials for pulping and fixing CO 2, has wide sources of raw materials, higher absorption rate and obvious carbon fixing process, and the absorption liquid is prepared from urban domestic sewage and organic wastewater containing citric acid and acetic acid, and is used for preparing waste by waste; |[0019] 2. The method of the invention utilizes the metabolism of compound microorganisms to produce products such as small molecular acid and the like, accelerates the decomposition of feldspar minerals and releases metal cations such as potassium and calcium into the absorption slurry, and improves the carbon fixation effect, meanwhile, the potassium in the feldspar minerals is converted into a soluble state and enters the absorption slurry, and the carbon fixation absorption slurry is suitable for the subsequent potassium extraction and utilization. |DRAWINGS DESCRIPTION|[0020] FIG. 1 is a schematic diagram of a carbon sequestration bioreactor and a pulping tank according to the present invention;|[0021] In the figure, a reactor body, a 2-spiral spray head, a 3-diversion inner cylinder, a 4-fixed frame body, a 5-carbon dioxide aeration device, a 6-evacuation pipe, a 7-velvet filler, an 8-return pipe, a 9-pulping tank, a 10-conveying pump, a 11-stirring device, a 12-waste slurry discharge port, a 13-observation and temporary feeding port, a 14-tail gas discharge port and a 15-air inlet buffer tank are arranged. |INVENTION MODE|Detailed Description|[0022] The invention is further illustrated, but is not limited in any way, by the following examples, and any alterations or substitutions based on the teachings of the invention are within the scope of the invention.|[0023] Example 1|[0024] Inoculating aspergillus aculeatus to a solid culture medium, preparing aspergillus aculeatus spore suspension, inoculating the aspergillus aculeatus to a liquid culture solution filled with velvet-shaped fillers, adjusting the pH value of the absorption slurry to 8.8 after uniformly stirring and mixing, taking out the fillers after film-forming culture, fixing the fillers to a fixed frame body of a guide inner cylinder of a reactor, wherein the mass ratio of the fillers to the absorption liquid in the reactor is 35:100, preparing the absorption liquid with the Chemical Oxygen Demand (COD) of 350mg/L by adopting municipal domestic sewage and organic wastewater containing citric acid, wherein the volume ratio of the organic wastewater is 5.0%, adding potassium feldspar crushed to be less than 100 mu m in a pulping tank according to the mass ratio of the absorption liquid, stirring and mixing uniformly, adjusting the pH value of the absorption slurry to 8.8, and then, feeding wet-based bacteria after proliferation culture into the reactor by using a conveying pump when the liquid level in the reactor reaches a specified height, wherein the consumption of the wet-based bacteria is 1.0% of the total mass of the absorption liquid, and carrying out silicate preparation in the pulping tank and the reactor at room temperature;|[0025] Mixing carbon dioxide with air, wherein the concentrations of CO 2 and O 2 in the mixed gas are 15% and 16% respectively, after a conveying pump is started, the mixed gas is fully contacted with absorption slurry in a diversion inner cylinder and drives to form an ascending flow, the gas continuously diffuses upwards after escaping from the liquid phase of an absorption system and is in countercurrent contact with circulating absorption slurry sprayed out of a spiral spray head at the upper part of a reactor, and tail gas is discharged through a discharge port; |[0026] When the pH value of the absorption system is reduced to 7.2, the Na, K and Ca concentrations in the circulating liquid are respectively 301, 130 and 14mg/L, the absorption efficiency of the CO 2 in the reaction device is reduced to 45 percent, compared with the absorption device without adding microorganisms, the time is shortened by 35 minutes when the K concentration in the circulating liquid is only 12mg/L, the absorption efficiency of the CO 2 is reduced to 41 percent and the pH value is reduced to the same value. |[0027] Example 2|[0028] Inoculating aspergillus aculeatus spore suspension into liquid culture solution filled with velvet-shaped filler, wherein the inoculation concentration is 1.0X10 6/mL, taking out the filler after film-forming culture, fixing the filler to a fixed frame body of a guide inner cylinder of a reactor, wherein the mass ratio of the filler to the absorption liquid in the reactor is 25:100, preparing the absorption liquid with the Chemical Oxygen Demand (COD) of 420mg/L by adopting municipal domestic sewage and organic wastewater containing acetic acid, wherein the volume ratio of the organic wastewater is 10.0%, adding potassium feldspar crushed to 75 mu m in a pulping tank according to the proportion of 4.5% of the mass of the absorption liquid, stirring and mixing, adjusting the pH value of the slurry to 9.5, feeding mixed gas with the CO 2 concentration of 6% into the reactor through an aeration device, and keeping the effective residence time of the gas in the reactor for about 6s, wherein the rest operation is the same as in the embodiment 1;|[0029] When the pH value of the absorption system is reduced to 8.0, the concentration of Na, K and Ca in the circulating liquid is 52 mg/L, 38 mg/L and 11mg/L respectively, the absorption efficiency of the reaction device CO 2 is 62 percent, compared with the absorption device without microorganism, the concentration of K in the circulating liquid is only 16mg/L and the absorption efficiency of CO 2 is 55 percent. |[0030] Example 3|[0031] According to the embodiment, domestic sewage and citric acid organic wastewater are blended to obtain mixed liquor with a COD value of 480mg/L, wherein the volume ratio of the organic wastewater is 4.0%, potassium feldspar and anorthite which are crushed to 75 mu m are added according to the mass ratio of 1.5% after the absorption liquor is added into a pulping tank, the mass ratio of the two kinds of feldspar is 1:1, the pH value of the obtained absorption liquor is 9.5, the obtained absorption liquor is sent into a reactor, the added and proliferated wet-base silicate bacteria are added, the dosage of the wet-base silicate bacteria is 0.5% of the total mass of the absorption liquor, and the rest operation is the same as that of the embodiment 1;|[0032] When the pH value of the absorption system is reduced to 7.5, the concentration of K, ca in the circulating liquid is 42 mg/L and the absorption efficiency of the reaction device CO 2 is 53 percent. Along with the continuous advancing of the absorption operation, when the pH value is reduced to 7.0, the concentration of K, ca in the circulating liquid is 58 mg/L and 8mg/L respectively, and the absorption efficiency of the CO 2 in the reaction device is reduced to 40.5%. |[0033] Example 4|[0034] In the embodiment, aspergillus aculeatus spore suspension is inoculated into liquid culture solution filled with velvet-shaped filler, the inoculation concentration is 0.2X10 6/mL, the filler is taken out and fixed to a fixed frame body of a guide inner cylinder of a reactor after film-forming culture, the mass ratio of the filler to absorption liquid in the reactor is 40:100, the absorption liquid with COD of 350mg/L is prepared by adopting domestic sewage and citric acid organic wastewater, then feldspar mineral mixture crushed to 100 mu m is added according to the mass ratio of 3.0%, the feldspar mineral mixture is obtained by mixing potassium feldspar, anorthite and biotite according to the mass ratio of 1:1:1, the pH value of the absorption slurry is not adjusted after the absorption slurry is prepared, and the absorption slurry is then sent to the reactor, and the rest operation is the same as in the embodiment 1.|[0035] When the pH value of the absorption system is lower than 7.2, the concentration of K, ca in the circulating liquid is 96 mg/L and 11mg/L respectively, the absorption efficiency of CO 2 in the reaction device is reduced to 42%, at the moment, 1/8 absorption slurry is discharged from the bottom of the pulping tank, then the equal volume of COD 350mg/L absorption liquid is supplemented, the feldspar mixed minerals are added at the same time, the dosage of the feldspar mixed minerals is equal to the solid matter content in the waste absorption slurry, and after the operation is carried out for 10min, the pH value of the absorption slurry in the reactor is increased to 8.1 again, and the absorption efficiency of CO 2 is 48.7%.|[0036] Example 5|[0037] This example was the same as example 1 except that the mass ratio of the filler to the absorption liquid in the reactor was 32.5:100, the solids content of the feldspar minerals in the absorption slurry was 4.5%, the chemical oxygen demand of the absorption liquid was controlled to 500mg/L, and the concentration of CO 2 was 0.5%; on the basis of the embodiment 1, the carbon-fixing bioreactor comprises a reactor body 1, a spiral spray head 2, a guide inner cylinder 3, a fixed frame body 4, a carbon dioxide aeration device 5 and an emptying pipe 6, wherein the spiral spray head 2 is arranged at the top in the reactor body 1, the guide inner cylinder 3 is arranged in the reactor body 1, the guide inner cylinder 3 is of a cylindrical structure, the inside of the guide inner cylinder 3 is hollow, the upper end and the lower end of the guide inner cylinder are both open, a space is reserved between the guide inner cylinder 3 and the inner wall of the reactor body 1, the fixed frame body 4 is arranged in the guide inner cylinder 3, the carbon dioxide aeration device 5 is arranged at the bottom in the reactor body 1, the emptying pipe 6 is arranged at the bottom of the reactor body 1, and the fixed frame body 4 is internally provided with a velvet-shaped filler 7; when in use, CO 2 gas is mixed with air and then is sent into the reactor body 1 through the carbon dioxide aeration device 5, the absorption slurry is in an ascending liquid state in the diversion inner cylinder 3, fully contacts with a biomembrane formed by microorganisms attached to and growing on the velvet-shaped filler 7 and microorganisms growing in suspension, and flows downwards along a space between the outer side of the diversion inner cylinder and the side wall of the reactor body 1 after the absorption slurry ascends, the method comprises the steps of flowing to the bottom of a reactor body 1, flowing absorption slurry into a pulping tank 9 (namely a circulating tank) through a return pipe 8, conveying the absorption slurry to a spiral spray head 2 through a conveying pump 10 and spraying the absorption slurry out, countercurrent contacting with CO 2 escaped from a liquid-phase absorption system in the reactor body 1 again, evacuating the absorption slurry through an evacuating pipe 6 when the system stops running, discharging a certain amount of absorption slurry from a waste slurry discharge port 12 at the bottom of the pulping tank 9 when the pH value of circulating liquid in the pulping tank 9 is lower than 7.2, supplementing an equal volume of absorption liquid and adding feldspar minerals, wherein the amount of the absorption liquid is 0.8 times the amount of solids in the waste absorption liquid, and continuously circulating.|[0038] Example 6|[0039] The embodiment is the same as that of the embodiment 5 except that the chemical oxygen demand of the absorption liquid is controlled to be 425mg/L, the concentration of CO 2 is 8.0%, on the basis of the embodiment 5, an observation and temporary feeding port 13 is arranged at the upper part of the side surface of the reactor body 1, a tail gas discharge port 14 is arranged at the top of the reactor body 1, a carbon dioxide aeration device 5 is communicated with an air inlet buffer tank 15 through an air pipeline, tail gas in the reactor body 1 is discharged through the tail gas discharge port 14, and when the system is started, the proliferated wet silicate bacteria can be added from the observation and temporary feeding port 13;|[0040] when the pH value of the absorption slurry in the reactor is lower than 7.2, quantitative absorption slurry is discharged from the bottom of the pulping tank, and then the fresh absorption slurry with the same volume is supplemented, and meanwhile, feldspar mineral is added, wherein the dosage of the feldspar mineral is 1.2 times of the solid content in the waste absorption liquid. (CN115591395)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of industrial tail gas purification and resource utilization, and particularly relates to a method for solidifying carbon by a composite microorganism reinforced feldspar mineral.|BACKGROUND ART|[0002] With the increasing demand of human society for fossil fuels, the carbon dioxide emission in industrial production process is rapidly increased, and the problem of greenhouse effect caused by carbon dioxide is widely focused. The main methods of capturing, sealing or fixing carbon dioxide commonly used at present are plant or algae absorption and conversion, physical adsorption, air separation/exhaust circulation method, chemical absorption method and the like. The chemical absorption method separates carbon dioxide from the mixed gas by utilizing chemical reaction between the carbon dioxide and the absorption slurry, and has the characteristics of large absorption capacity, good absorption effect, lower cost and the like, so that the method is more focused in practical application.|[0003] The prior patent CN109261116A uses zirconium oxynitrate as a zirconium source, lithium hydroxide as a lithium source, carbonate as a precipitator, and carries out precipitation reaction in ammonia water solution, filtering or evaporating to remove water after the reaction, and then drying and roasting to obtain the lithium zirconate adsorption material. The prior patent CN107902631A uniformly mixes pretreated potassium feldspar powder, carbon powder and calcium sulfate, tabletting and forming, and collecting sulfur dioxide after high-temperature activation reaction under nitrogen atmosphere, mineralizing and calcining slag by adopting CO2, and separating and obtaining mineralized slag containing calcium carbonate and water-soluble potassium sulfate fertilizer. However, the method needs to add a large amount of exogenous agents, and the operation cost of the mineralized carbon fixation process is obviously increased. In natural environment, silicate substances and metal cations such as calcium, iron and the like are generated after the feldspar minerals are decomposed, and dissolved metal cations react with carbon dioxide to generate indissolvable carbonate, but the progress of carbon fixation through the above approaches is very slow. The development of efficient and cost-effective carbon sequestration technology has significant implications for implementation of new-period two-carbon action plans.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a method for strengthening carbon fixation of feldspar minerals by composite microorganisms, which comprises the steps of pulping the feldspar minerals, adding the pulped feldspar minerals into a carbon fixation bioreactor, constructing a composite microorganism system with coexistent suspension and adhesion growth states, bubbling CO 2 from the bottom of the reactor and fully contacting with a biological membrane and suspended microorganisms, dissolving out metal cations such as calcium and iron dissolved in the feldspar minerals and reacting with CO 2, and finally converting the dissolved metal cations into insoluble carbonate for precipitation so as to achieve the aim of carbon fixation, wherein after aspergillus aculeatus and silicate bacteria are added into the reactor, the content of metabolites such as small molecular acid in an absorption liquid is higher, accelerating the decomposition of the feldspar minerals and releasing metal cations such as potassium into the absorption liquid, thereby improving the effect of carbon fixation and potassium release.|[0005] The object of the invention is achieved in that it comprises the following steps:|[0006] s1, loading aspergillus aculeatus into a velvet-shaped filler, fixing the filler to a fixed frame body of a guide inner cylinder of a carbon-fixing bioreactor, and simultaneously adding silicate bacteria after multiplication culture into the reactor, wherein feldspar minerals are crushed to a particle size of less than 100 mu m, then uniformly mixed with an absorption liquid in a pulping tank to prepare absorption slurry, and then pumped into the reactor containing aspergillus aculeatus and silicate bacteria; |[0007] S2, CO 2 is sent into the reactor through an aeration device at the bottom of the carbon-fixing bioreactor, fully contacts with absorption slurry in the guide inner cylinder and is in an ascending flow state, and fully contacts with biological membranes and suspended microorganisms, then the absorption slurry flows downwards to the bottom of the reactor in a space between the outer side of the guide inner cylinder and the inner side of the reactor and is discharged, the discharged absorption slurry is conveyed by a conveying pump, is sprayed out from a spiral spray head at the inner top of the reactor and is in countercurrent contact with CO 2 escaped from a liquid-phase absorption system in the reactor, and CO 2 is finally converted into carbonate sediment and is discharged. |[0008] Preferably, the silicate bacteria are cultured by leaching root system soil in a bud stage by using 0.5% of citric acid, adding potassium feldspar mineral powder according to the mass of leaching solution of 0.5%, culturing for 7 days under the condition of pH of 7.5, centrifuging to collect wet-base bacteria, and adding the silicate bacteria into a reactor according to the proportion of 0.6-1.5% of the total mass of absorption liquid.|[0009] Preferably, the aspergillus aculeatus is inoculated into a solid culture medium to prepare an aspergillus aculeatus spore suspension, then the aspergillus aculeatus is inoculated into a liquid culture solution filled with velvet-shaped fillers, the inoculation concentration is 0.1-1 multiplied by 10 6/mL, the membrane is hung for 3 days for culture, then the fillers are taken out, the fillers are fixed to a fixed frame body of a guide inner cylinder of a reactor after being taken out, and the mass ratio of the fillers to an absorption liquid is 25-40:100.|[0010] Preferably, the feldspar mineral is one or more of potassium feldspar, anorthite or biotite, and the solid content of the feldspar mineral in the absorption slurry is 1.5-4.5%, wherein the percentage is the mass percentage.|[0011] Preferably, the absorption liquid is prepared from urban domestic sewage and organic wastewater containing citric acid and acetic acid, and the chemical oxygen demand of the absorption liquid is controlled to be 350-500 mg/L.|[0012] Preferably, the concentration of CO 2 fed into the reactor is 0.5-15% (volume percent), the oxygen content is not less than 15% (volume percent), and the residence time of the gas in the absorption system is 5-15 s.|[0013] Preferably, the pH value of the absorption slurry in the reactor is controlled to be 7.2-9.5, when the pH value is lower than 7.2, quantitative absorption slurry is discharged from the bottom of the pulping tank, then the equal volume of fresh absorption slurry is supplemented, and meanwhile feldspar minerals are added, wherein the dosage of the feldspar minerals is 0.8-1.2 times of the solid content in the waste absorption liquid.|[0014] Preferably, the quantitative absorption slurry accounts for 10-20% of the total absorption slurry by mass.|[0015] Preferably, the carbon-fixing bioreactor comprises a reactor body, a spiral spray head, a guide inner cylinder, a fixed frame body, a carbon dioxide aeration device and an emptying pipe, wherein the spiral spray head is arranged at the top of the reactor body, the guide inner cylinder is arranged in the reactor body and is of a cylindrical structure, the inside of the reactor body is hollow, the upper end and the lower end of the reactor body are open, a space is reserved between the guide inner cylinder and the inner wall of the reactor body, the fixed frame body is arranged in the guide inner cylinder, the carbon dioxide aeration device is arranged at the bottom of the reactor body, the emptying pipe is arranged at the bottom of the reactor body, a velvet-shaped filler is filled in the fixed frame body, the bottom of the reactor body is communicated with the bottom of a pulping tank through a return pipe, the pulping tank is communicated with the spiral spray head through a conveying pipe, a conveying pump is arranged in the conveying pump, and a stirring device is arranged in the pulping tank, and the bottom of the pulping tank is provided with a waste slurry discharge port.|[0016] Preferably, the upper part of the side surface of the reactor body is provided with an observation and temporary feeding port, the top of the reactor body is provided with a tail gas discharge port, and the carbon dioxide aeration device is communicated with the air inlet buffer tank through a gas pipeline.|[0017] Compared with the prior art, the invention has the following technical effects:|[0018] 1. The method takes feldspar minerals as raw materials for pulping and fixing CO 2, has wide sources of raw materials, higher absorption rate and obvious carbon fixing process, and the absorption liquid is prepared from urban domestic sewage and organic wastewater containing citric acid and acetic acid, and is used for preparing waste by waste; |[0019] 2. The method of the invention utilizes the metabolism of compound microorganisms to produce products such as small molecular acid and the like, accelerates the decomposition of feldspar minerals and releases metal cations such as potassium and calcium into the absorption slurry, and improves the carbon fixation effect, meanwhile, the potassium in the feldspar minerals is converted into a soluble state and enters the absorption slurry, and the carbon fixation absorption slurry is suitable for the subsequent potassium extraction and utilization. |DRAWINGS DESCRIPTION|[0020] FIG. 1 is a schematic diagram of a carbon sequestration bioreactor and a pulping tank according to the present invention;|[0021] In the figure, a reactor body, a 2-spiral spray head, a 3-diversion inner cylinder, a 4-fixed frame body, a 5-carbon dioxide aeration device, a 6-evacuation pipe, a 7-velvet filler, an 8-return pipe, a 9-pulping tank, a 10-conveying pump, a 11-stirring device, a 12-waste slurry discharge port, a 13-observation and temporary feeding port, a 14-tail gas discharge port and a 15-air inlet buffer tank are arranged. |INVENTION MODE|Detailed Description|[0022] The invention is further illustrated, but is not limited in any way, by the following examples, and any alterations or substitutions based on the teachings of the invention are within the scope of the invention.|[0023] Example 1|[0024] Inoculating aspergillus aculeatus to a solid culture medium, preparing aspergillus aculeatus spore suspension, inoculating the aspergillus aculeatus to a liquid culture solution filled with velvet-shaped fillers, adjusting the pH value of the absorption slurry to 8.8 after uniformly stirring and mixing, taking out the fillers after film-forming culture, fixing the fillers to a fixed frame body of a guide inner cylinder of a reactor, wherein the mass ratio of the fillers to the absorption liquid in the reactor is 35:100, preparing the absorption liquid with the Chemical Oxygen Demand (COD) of 350mg/L by adopting municipal domestic sewage and organic wastewater containing citric acid, wherein the volume ratio of the organic wastewater is 5.0%, adding potassium feldspar crushed to be less than 100 mu m in a pulping tank according to the mass ratio of the absorption liquid, stirring and mixing uniformly, adjusting the pH value of the absorption slurry to 8.8, and then, feeding wet-based bacteria after proliferation culture into the reactor by using a conveying pump when the liquid level in the reactor reaches a specified height, wherein the consumption of the wet-based bacteria is 1.0% of the total mass of the absorption liquid, and carrying out silicate preparation in the pulping tank and the reactor at room temperature;|[0025] Mixing carbon dioxide with air, wherein the concentrations of CO 2 and O 2 in the mixed gas are 15% and 16% respectively, after a conveying pump is started, the mixed gas is fully contacted with absorption slurry in a diversion inner cylinder and drives to form an ascending flow, the gas continuously diffuses upwards after escaping from the liquid phase of an absorption system and is in countercurrent contact with circulating absorption slurry sprayed out of a spiral spray head at the upper part of a reactor, and tail gas is discharged through a discharge port; |[0026] When the pH value of the absorption system is reduced to 7.2, the Na, K and Ca concentrations in the circulating liquid are respectively 301, 130 and 14mg/L, the absorption efficiency of the CO 2 in the reaction device is reduced to 45 percent, compared with the absorption device without adding microorganisms, the time is shortened by 35 minutes when the K concentration in the circulating liquid is only 12mg/L, the absorption efficiency of the CO 2 is reduced to 41 percent and the pH value is reduced to the same value. |[0027] Example 2|[0028] Inoculating aspergillus aculeatus spore suspension into liquid culture solution filled with velvet-shaped filler, wherein the inoculation concentration is 1.0X10 6/mL, taking out the filler after film-forming culture, fixing the filler to a fixed frame body of a guide inner cylinder of a reactor, wherein the mass ratio of the filler to the absorption liquid in the reactor is 25:100, preparing the absorption liquid with the Chemical Oxygen Demand (COD) of 420mg/L by adopting municipal domestic sewage and organic wastewater containing acetic acid, wherein the volume ratio of the organic wastewater is 10.0%, adding potassium feldspar crushed to 75 mu m in a pulping tank according to the proportion of 4.5% of the mass of the absorption liquid, stirring and mixing, adjusting the pH value of the slurry to 9.5, feeding mixed gas with the CO 2 concentration of 6% into the reactor through an aeration device, and keeping the effective residence time of the gas in the reactor for about 6s, wherein the rest operation is the same as in the embodiment 1;|[0029] When the pH value of the absorption system is reduced to 8.0, the concentration of Na, K and Ca in the circulating liquid is 52 mg/L, 38 mg/L and 11mg/L respectively, the absorption efficiency of the reaction device CO 2 is 62 percent, compared with the absorption device without microorganism, the concentration of K in the circulating liquid is only 16mg/L and the absorption efficiency of CO 2 is 55 percent. |[0030] Example 3|[0031] According to the embodiment, domestic sewage and citric acid organic wastewater are blended to obtain mixed liquor with a COD value of 480mg/L, wherein the volume ratio of the organic wastewater is 4.0%, potassium feldspar and anorthite which are crushed to 75 mu m are added according to the mass ratio of 1.5% after the absorption liquor is added into a pulping tank, the mass ratio of the two kinds of feldspar is 1:1, the pH value of the obtained absorption liquor is 9.5, the obtained absorption liquor is sent into a reactor, the added and proliferated wet-base silicate bacteria are added, the dosage of the wet-base silicate bacteria is 0.5% of the total mass of the absorption liquor, and the rest operation is the same as that of the embodiment 1;|[0032] When the pH value of the absorption system is reduced to 7.5, the concentration of K, ca in the circulating liquid is 42 mg/L and the absorption efficiency of the reaction device CO 2 is 53 percent. Along with the continuous advancing of the absorption operation, when the pH value is reduced to 7.0, the concentration of K, ca in the circulating liquid is 58 mg/L and 8mg/L respectively, and the absorption efficiency of the CO 2 in the reaction device is reduced to 40.5%. |[0033] Example 4|[0034] In the embodiment, aspergillus aculeatus spore suspension is inoculated into liquid culture solution filled with velvet-shaped filler, the inoculation concentration is 0.2X10 6/mL, the filler is taken out and fixed to a fixed frame body of a guide inner cylinder of a reactor after film-forming culture, the mass ratio of the filler to absorption liquid in the reactor is 40:100, the absorption liquid with COD of 350mg/L is prepared by adopting domestic sewage and citric acid organic wastewater, then feldspar mineral mixture crushed to 100 mu m is added according to the mass ratio of 3.0%, the feldspar mineral mixture is obtained by mixing potassium feldspar, anorthite and biotite according to the mass ratio of 1:1:1, the pH value of the absorption slurry is not adjusted after the absorption slurry is prepared, and the absorption slurry is then sent to the reactor, and the rest operation is the same as in the embodiment 1.|[0035] When the pH value of the absorption system is lower than 7.2, the concentration of K, ca in the circulating liquid is 96 mg/L and 11mg/L respectively, the absorption efficiency of CO 2 in the reaction device is reduced to 42%, at the moment, 1/8 absorption slurry is discharged from the bottom of the pulping tank, then the equal volume of COD 350mg/L absorption liquid is supplemented, the feldspar mixed minerals are added at the same time, the dosage of the feldspar mixed minerals is equal to the solid matter content in the waste absorption slurry, and after the operation is carried out for 10min, the pH value of the absorption slurry in the reactor is increased to 8.1 again, and the absorption efficiency of CO 2 is 48.7%.|[0036] Example 5|[0037] This example was the same as example 1 except that the mass ratio of the filler to the absorption liquid in the reactor was 32.5:100, the solids content of the feldspar minerals in the absorption slurry was 4.5%, the chemical oxygen demand of the absorption liquid was controlled to 500mg/L, and the concentration of CO 2 was 0.5%; on the basis of the embodiment 1, the carbon-fixing bioreactor comprises a reactor body 1, a spiral spray head 2, a guide inner cylinder 3, a fixed frame body 4, a carbon dioxide aeration device 5 and an emptying pipe 6, wherein the spiral spray head 2 is arranged at the top in the reactor body 1, the guide inner cylinder 3 is arranged in the reactor body 1, the guide inner cylinder 3 is of a cylindrical structure, the inside of the guide inner cylinder 3 is hollow, the upper end and the lower end of the guide inner cylinder are both open, a space is reserved between the guide inner cylinder 3 and the inner wall of the reactor body 1, the fixed frame body 4 is arranged in the guide inner cylinder 3, the carbon dioxide aeration device 5 is arranged at the bottom in the reactor body 1, the emptying pipe 6 is arranged at the bottom of the reactor body 1, and the fixed frame body 4 is internally provided with a velvet-shaped filler 7; when in use, CO 2 gas is mixed with air and then is sent into the reactor body 1 through the carbon dioxide aeration device 5, the absorption slurry is in an ascending liquid state in the diversion inner cylinder 3, fully contacts with a biomembrane formed by microorganisms attached to and growing on the velvet-shaped filler 7 and microorganisms growing in suspension, and flows downwards along a space between the outer side of the diversion inner cylinder and the side wall of the reactor body 1 after the absorption slurry ascends, the method comprises the steps of flowing to the bottom of a reactor body 1, flowing absorption slurry into a pulping tank 9 (namely a circulating tank) through a return pipe 8, conveying the absorption slurry to a spiral spray head 2 through a conveying pump 10 and spraying the absorption slurry out, countercurrent contacting with CO 2 escaped from a liquid-phase absorption system in the reactor body 1 again, evacuating the absorption slurry through an evacuating pipe 6 when the system stops running, discharging a certain amount of absorption slurry from a waste slurry discharge port 12 at the bottom of the pulping tank 9 when the pH value of circulating liquid in the pulping tank 9 is lower than 7.2, supplementing an equal volume of absorption liquid and adding feldspar minerals, wherein the amount of the absorption liquid is 0.8 times the amount of solids in the waste absorption liquid, and continuously circulating.|[0038] Example 6|[0039] The embodiment is the same as that of the embodiment 5 except that the chemical oxygen demand of the absorption liquid is controlled to be 425mg/L, the concentration of CO 2 is 8.0%, on the basis of the embodiment 5, an observation and temporary feeding port 13 is arranged at the upper part of the side surface of the reactor body 1, a tail gas discharge port 14 is arranged at the top of the reactor body 1, a carbon dioxide aeration device 5 is communicated with an air inlet buffer tank 15 through an air pipeline, tail gas in the reactor body 1 is discharged through the tail gas discharge port 14, and when the system is started, the proliferated wet silicate bacteria can be added from the observation and temporary feeding port 13;|[0040] when the pH value of the absorption slurry in the reactor is lower than 7.2, quantitative absorption slurry is discharged from the bottom of the pulping tank, and then the fresh absorption slurry with the same volume is supplemented, and meanwhile, feldspar mineral is added, wherein the dosage of the feldspar mineral is 1.2 times of the solid content in the waste absorption liquid. Family Number|(103441127)|103441127|Abstract|(CN115591395B B)|The invention discloses a method for enhancing carbon sequestration of feldspar minerals by compound microorganisms , which comprises the following steps : crushing feldspar minerals , pulping , pumping into a carbon sequestration bioreactor containing aspergillus and silicate bacteria , and absorbing slurry in an upflow state in a flow guide inner cylinder of the reactor , then downwards reflowing to the bottom of the reactor along a space between the outer side of the flow guide inner cylinder and the inner wall of the reactor ; cO2 is blown in from the bottom of the reactor and is in full contact with a biological membrane and suspended microorganisms , the CO2 is dissolved in absorption slurry and reacts with metal cations dissolved out of feldspar minerals , finally , the CO2 is converted into indissolvable carbonate precipitates , and the purpose of carbon sequestration is achieved . According to the method , the feldspar mineral is used as the raw material for pulping and fixing CO2 , the raw material source is wide , the absorption rate is high , and the carbon fixation process is obvious ; products such as small molecular acid are generated by metabolism of the compound microorganisms , decomposition of feldspar minerals is accelerated , metal cations are released into absorption slurry , potassium in the feldspar minerals is converted into a soluble state , subsequent potassium extraction is facilitated , and the dual effects of carbon sequestration and potassium release are achieved . |CPC codes|(CN115591395B B)|B01D - 053/62 |B01D - 053/78 |B01D - 053/84 |C01F - 011/18 |IPC codes|(CN115591395B B)|B01D - 053/62 |B01D - 053/78 |B01D - 053/84 |C01F - 011/18 |Title|(CN115591395 A)|Method for reinforcing feldspar mineral carbon sequestration through compound microorganisms | Environmental technology|Materials, metallurgy B01D-053/50/2|B01D-053/62|B01D-053/78|B01D-053/84|B01D-053/96|B01D-2251/304|B01D-2251/404|B01D-2251/604|B01D-2257/504|B01D-2258/0283|B01D-2259/124|C01F-011/18|C01F-011/46/4|Y02A-050/2342|Y02A-050/2358|Y02C-010/02|Y02C-010/04|Y02C-010/06|Y02C-020/40|Y02P-020/152|Y02P-020/59 B01D-053/50/2|B01D-053/62|B01D-053/78|B01D-053/84|B01D-053/96|B01D-2251/304|B01D-2251/404|B01D-2251/604|B01D-2257/504|B01D-2258/0283|B01D-2259/124|C01F-011/18|C01F-011/46/4|Y02A-050/2342|Y02A-050/2358|Y02C-010/02|Y02C-010/04|Y02C-010/06|Y02C-020/40|Y02P-020/152|Y02P-020/59 B01D-053/62|B01D-053/78|B01D-053/84|C01F-011/18 B01D-053/62|B01D-053/78|B01D-053/84|C01F-011/18 CN116161660|WO2024169718|KR20250074239|KR102886625 CN116161660 105090822 WHO=Examiner SELF=N CAT=Y|WO2024169718 105090822 WHO=Examiner SELF=N CAT=A|KR20250074239 114710636 WHO=Examiner SELF=N|KR102886625 114710636 WHO=Examiner SELF=N CN104353343|CN102701253|CN103221116|CN102343199|CN101992020|US20060257281|EP1009795|CN108690813|CN104524967|CN102491795 CN104353343 68620669 WHO=Examiner SELF=N CAT=A|CN102701253 7910585 WHO=Examiner SELF=N CAT=A|CN103221116 17025569 WHO=Examiner SELF=N CAT=A|CN102343199 7520860 WHO=Examiner SELF=N CAT=A|CN101992020 7239135 WHO=Examiner SELF=N CAT=A|US20060257281 904564 WHO=Examiner SELF=N CAT=A|EP1009795 577888 WHO=Examiner SELF=N CAT=A|CN108690813 81714831 WHO=Examiner SELF=N|CN104524967 69125392 WHO=Examiner SELF=N|CN102491795 7714494 WHO=Examiner SELF=N 李永;李福春;杨刚;胡若愚;: &quot;真菌与细菌作用下黑云母中主要元素溶出状况的对比分析&quot;, 土壤通报, no. 01, 6 February 2017 (2017-02-06) (Cat. A) CN101992020; CN102343199; CN102701253; CN103221116; CN104353343; EP1009795; US20060257281; CN102491795; CN108690813; CN104524967 GRANTED (CN115591395)|GRANTED ALIVE (CN115591395)|ALIVE (CN115591395)|LEGAL DETAILS FOR CN115591395|Actual or expected expiration date=2042-09-07|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-09-07|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211087853|Application date=2022-09-07|Standardized application number=2022CN-1087853|Event publication date=2023-01-13|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115591395|Publication stage code=A|Publication date=2023-01-13|Standardized publication number=CN115591395|Event publication date=2023-01-13|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-02-07|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-08-08|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN115591395|Publication stage code=B|Publication date=2025-08-08|Standardized publication number=CN115591395B|Event publication date=2025-08-08|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN115591395)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRHCYIPUdBUNhj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000078515358&ekey=2152&xpn=CN115591395B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=MWATEmtXmvrHTw0qN%252FwR6LmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN115591395)|CN|(CN115591395)|CN (CN115591395)|NAME=KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN|(CN115591395)|NAME=KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN115591395)|NAME=ZHANG YANG;Kunming Tongju Patent Agency Co., Ltd. , REG=53214NAME=ZHANG YU;Kunming Tongju Patent Agency Co., Ltd. , REG=53214|(CN115591395)|NAME=ZHANG YANG;Kunming Tongju Patent Agency Co., Ltd. , REG=53214NAME=ZHANG YU;Kunming Tongju Patent Agency Co., Ltd. , REG=53214 (CN115591395)|CN| (CN115591395)|NAME=LIU SHUGEN, COUNTRY=CN |NAME=YE FUYING|NAME=WANG QIONGHUI|NAME=PENG YUXIN|NAME=TIAN SENLIN|NAME=NING PING|NAME=SHI JIANWU|(CN115591395)|NAME=LIU SHUGEN|NAME=YE FUYING|NAME=WANG QIONGHUI|NAME=PENG YUXIN|NAME=TIAN SENLIN|NAME=NING PING|NAME=SHI JIANWU 0 1 Titre: (CN115591395)|Method for strengthening carbon fixation of feldspar mineral by composite microorganisms Résumé: (CN115591395)|The invention discloses a method for enhancing carbon sequestration of feldspar minerals by compound microorganisms, which comprises the following steps: crushing feldspar minerals, pulping, pumping into a carbon sequestration bioreactor containing aspergillus and silicate bacteria, and absorbing slurry in an upflow state in a flow guide inner cylinder of the reactor, then downwards reflowing to the bottom of the reactor along a space between the outer side of the flow guide inner cylinder and the inner wall of the reactor; cO2 is blown in from the bottom of the reactor and is in full contact with a biological membrane and suspended microorganisms, the CO2 is dissolved in absorption slurry and reacts with metal cations dissolved out of feldspar minerals, finally, the CO2 is converted into indissolvable carbonate precipitates, and the purpose of carbon sequestration is achieved. According to the method, the feldspar mineral is used as the raw material for pulping and fixing CO2, the raw material source is wide, the absorption rate is high, and the carbon fixation process is obvious; products such as small molecular acid are generated by metabolism of the compound microorganisms, decomposition of feldspar minerals is accelerated, metal cations are released into absorption slurry, potassium in the feldspar minerals is converted into a soluble state, subsequent potassium extraction is facilitated, and the dual effects of carbon sequestration and potassium release are achieved. 36 Abstract gpt-4o-mini yes The article describes a method for enhancing carbon sequestration using feldspar minerals and microorganisms, which aligns with the topic of accelerated weathering and CO₂ capture.
39 US63/669,351P|US19/264,502 US19/264,502 US20260017435 117356463 US20260017435 A1 2026-01-15 [US20260017435] 2024-07-10|2025-07-09 2025-07-09 2026-01-15 (US20260017435)|2045-07-09 (US20260017435)|Technologies for modeling carbon dioxide removal (US20260017435)|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed. UNIVERSITY INDIANA TRUSTEES (US20260017435)|THE TRUSTEES OF INDIANA UNIVERSITY ([US]) ZHU CHEN (US20260017435)|Zhu Chen (US20260017435)|A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring.|There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein.|Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.| (US20260017435)|1. A compute device comprising: circuitry configured to: obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and present a visual representation of the at least one prediction in a user interface.|14. A method comprising: obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and presenting, by the compute device, a visual representation of the at least one prediction in a user interface.|19. One or more machine-readable storage media comprising a plurality of instructions stored thereon that, in response to being executed, cause a compute device to: obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and present a visual representation of the at least one prediction in a user interface.| (US20260017435)|Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.|In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV).|The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering.| (US20260017435)|ENHANCED ROCK(100,28)|MODELING CARBON DIOXIDE REMOVAL(100,6)|IRON COPRECIPITATION(94,11)|FORECAST MODEL(65,1)|FORECASTING MODEL(65,1)|VISUAL REPRESENTATION(59,20)|WORKFLOW EXECUTION(57,1)|NATIONAL OPEN CYBER INFRASTRUCTURE(56,1)|SATISFYING CONCERN(54,1)|PARAMETER DATA(53,57)|OPEN CYBER INFRASTRUCTURE(47,1)|GEOCHEMICAL MODEL(41,3)|CONCEPTUALIZATION(36,1)|CARBON DIOXIDE(33,77)|CLONABILITY(32,1)|REUSABILITY(32,1)|NEGOTIATION(31,1)|PROVENANCE(31,1)|POST PROJECT MONITORING(30,1)|ENHANCE REMOVAL(28,1)|VERIFICATION(28,1)|REPORTING(27,1)|SCIENCE GATEWAY(27,1)|COMPUTE DEVICE(26,45)|BASALT WEATHERING(25,6)|PUBLIC CLOUD(25,1)|MODELING COMPUTE DEVICE(24,92)|UNIDIRECTIONAL RATE(24,6)|SOILS(23,1)|GROUND(22,45)|CARBON DIOXIDE REMOVAL(22,12)|GATEWAY(21,15)|TOXIC METAL(20,24)|PREDICTION VISUAL REPRESENTATION(19,5)|USER INTERFACE(16,21)|LIBRARY(15,7)|IRREVERSIBLE REACTION(15,6)|MACHINE LEARNING MODEL(15,4)|STORAGE MEDIA(14,3)|HECTARE(13,12)|BASALT TON(12,2)|TOXIC METAL RELEASE(12,2)|NEAR EQUILIBRIUM RATE(11,5)|DATABASE(10,15)|LOCATION DISTANCE(10,4)|BLIND PORE(10,3)|INTERACTIVE GRAPH(10,3)|SOIL PARAMETER(10,3)|NICKEL VISUAL REPRESENTATION(10,2)|ACOUSTIC TOUCHSCREEN SENSOR(10,1)|ENHANCED ROCK WEATHERING BATCH(10,1)|SANDSTONE AQUIFER(10,1)|SEMIEMPIRICAL SCALING FACTOR(10,1)|WORLDWIDE INTEROPERABILITY(10,1)|SUBSYSTEM(9,7)|COMMUNICATION CIRCUITRY(9,6)|OBTAINING PARAMETER DATA(9,6)|PREDICTED(9,6)|PROBABILITY(8,5)|BASALT DENSITY(8,3)|TOPSOIL LAYER(8,3)|CYBER INFRASTRUCTURE(8,1)|GEOCHEMICAL EXPERT(8,1)|INFRARED TOUCHSCREEN SENSOR(8,1)|LEVERAGE EXPERTIZE(8,1)|MINE TAILING(8,1)|RENDING ENGINE(8,1)|WEB INTERFACE(7,5)|BULK SOIL DENSITY(7,4)|APPLICABLE REGULATION(7,2)|NONVOLATILE MEMORY(7,2)|SOIL DEPTH(7,2)|BASALT MINERAL MAKEUP(7,1)|GRAPHICAL PRESENTATION(7,1)|INTERPRETABLE MODEL(7,1)|MULTICHIP PACKAGE(7,1)|NUMB INDICATIVE(7,1)|PORTABLE NETWORK GRAPHICS(7,1)|PURCHASER CORPORATION(7,1)|RECONFIGURABLE HARDWARE(7,1)|SIMILARITY SCORE(7,1)|SIMILARITY DETERMINATION(6,3)|STAKEHOLDER(6,3)|AUTOMATIC DOCUMENTATION(6,1)|BASALT MASS(6,1)|BIODIVERSITY LOSS(6,1)|CAPACITIVE TOUCHSCREEN SENSOR(6,1)|CLUSTERING ANALYSIS(6,1)|ENCODED INSTRUCTION(6,1)|GROWING CONCERN(6,1)|IRRIGATION WATER REGULATION(6,1)|OXY HYDROXIDE(6,1)|PARAMETER DATA REFORMATTING(6,1)|RESISTIVE TOUCHSCREEN SENSOR(6,1)|SIMULATION CONFIDENCE INTERVAL(6,1)|SOIL REGULATION(6,1)|SPECIALIZED HARDWARE(6,1)|VISUAL PRESENTATION(6,1)|CADMIUM(5,4)|CHROMIUM(5,4)|AIR CALCULATION(5,2)|CUBIC CENTIMETER(5,2)|DRINKING WATER REGULATION(5,2)|GEOCHEMICAL MODELING(5,2)|GEOGRAPHIC COORDINATE(5,2)|NONEXPERT(5,2)|PHREEQC(5,2)|CARBON CAPTURE PREDICTION(5,1)|CARBON CAPTURE SIMULATION(5,1)|CARBON CREDIT MARKET(5,1)|COAXIAL NETWORK(5,1)|COMPLEX INTERACTION(5,1)|CONTROLLER CHIP(5,1)|CREDIT ABILITY(5,1)|DIGITAL VERSION(5,1)|ENHANCE CAPTURE(5,1)|FEED STOCK(5,1)|FILE FORMAT(5,1)|FIRMWARE CODE(5,1)|HARDWARE CIRCUITRY(5,1)|MICROWAVE ACCESS(5,1)|OPTICAL IMAGING TOUCHSCREEN SENSOR(5,1)|PREDICATION(5,1)|SIMULATION PRODUCT(5,1)|WEB MODEL INTERFACE(5,1)|GRAM(4,3)|USER INPUT(4,3)|PREDICTION ACCURACY(4,2)|ADJUSTED PARAMETER(3,1)|ARCHIVE(3,1)|AUTHORIZATION(3,1)|BLUETOOTH(3,1)|BUS LINK(3,1)|CARBON DIOXIDE TRAP ENERGY(3,1)|CERTIFICATION(3,1)|CHIPSET(3,1)|COPRECIPITATION(3,1)|COSINE SIMILARITY(3,1)|DAUGHTER CARD(3,1)|DISRUPTION(3,1)|DROUGHT(3,1)|ENCODING(3,1)|ENSEMBLE(3,1)|EXECUTABLE(3,1)|FACILITY(3,1)|FIBER NETWORK(3,1)|FIND PATTERN(3,1)|FLOODING(3,1)|GEOLOGICAL SURVEY(3,1)|GESTURE(3,1)|GIGATON LEVEL(3,1)|GREENHOUSE GAS ATMOSPHERE(3,1)|HYPERTEXT MARKUP LANGUAGE(3,1)|IDENTIFICATION(3,1)|INCLUSION(3,1)|INDUSTRY STANDARD AUTHENTICATION(3,1)|INTEGRATED SENSOR HUB(3,1)|KEYBOARD(3,1)|LYSIMETER EXPERIMENTAL DATA(3,1)|MAKE MODELING(3,1)| (US20260017435)|1. A compute device comprising:| circuitry configured to:| obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;| produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and| present a visual representation of the at least one prediction in a user interface.|2. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to simulate basalt weathering as irreversible reactions with unidirectional rates.|3. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates.|4. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to utilize one or more models that simulate co-precipitation of iron with toxic metals.|5. The compute device of claim 1, wherein to obtain parameter data comprises to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured.|6. The compute device of claim 1, wherein to obtain parameter data comprises to obtain the parameter data as a function of an identification of the location where the carbon dioxide is to be captured.|7. The compute device of claim 1, wherein the circuitry is further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models.|8. The compute device of claim 1, wherein to produce at least one prediction comprises to select one or more models as a function of the obtained parameter data.|9. The compute device of claim 1, wherein to produce at least one prediction comprises to select one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library.|10. The compute device of claim 1, wherein to produce at least one prediction comprises to utilize one or more machine learning models.|11. The compute device of claim 1, wherein to produce at least one prediction comprises to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.|12. The compute device of claim 1, wherein to produce at least one prediction comprises to produce one or more predictions indicative of tons of carbon dioxide captured per unit of area.|13. The compute device of claim 1, wherein to produce at least one prediction comprises to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured.|14. A method comprising:| obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;| producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and| presenting, by the compute device, a visual representation of the at least one prediction in a user interface.|15. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises simulating basalt weathering as irreversible reactions with unidirectional rates.|16. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates.|17. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises utilizing one or more models that simulate co-precipitation of iron with toxic metals.|18. The method of claim 14, wherein obtaining parameter data comprises obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured.|19. One or more machine-readable storage media comprising a plurality of instructions stored thereon that, in response to being executed, cause a compute device to:| obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;| produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and| present a visual representation of the at least one prediction in a user interface.|20. The one or more machine-readable storage media of claim 19, wherein to obtain parameter data comprises to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured. (US20260017435)|CROSS-REFERENCE TO RELATED APPLICATIONS|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/669,351 filed on Jul. 10, 2024, the disclosure of which is expressly incorporated herein.|(US20260017435)|BACKGROUND|[0002] Climate change is a growing concern across the world as atmospheric greenhouse gases such as carbon dioxide trap energy radiated from the sun. While a direct result of increases in greenhouse gases is increased temperatures on Earth, knock on effects include droughts, flooding, loss of biodiversity, and disruptions in energy and transportation systems across the world. Through interactions between water and rock (e.g., in soil), carbon dioxide can be captured (e.g., removed) from the atmosphere and correspondingly lessen the effects of climate change. However, given the multitude of factors that influence the complex interactions between water and rock, it is not feasible in conventional computerized systems to reliably determine the amount of carbon dioxide that will be removed in a given location, under a given set of conditions, or to predict side effects of any efforts to enhance the capture of carbon dioxide in the soil. Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.|SUMMARY|[0003] The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:|[0004] According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may be further configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. Producing a prediction may include simulating co-precipitation of iron with one or more toxic metals. The circuitry may be further configured to present a visual representation of the at least one prediction in a user interface.|[0005] In some embodiments, the circuitry may be configured such that using one or more models from a library of models to produce at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. The circuitry may also be configured to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, the circuitry may be configured to utilize one or more models that simulate co-precipitation of iron with toxic metals. The circuitry may be configured to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that obtaining data indicative of properties of soil includes obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and basalt mineral composition.|[0006] The circuitry may be configured such that obtaining parameter data includes obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured to obtain parameter data as a function of an identification of the location where the carbon dioxide is to be captured by reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. The circuitry may be configured to obtain parameter data through user input into corresponding fields of a user interface. In some embodiments, the circuitry may be further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models. The circuitry may be configured such that calculating additional parameter data involves calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.|[0007] In some embodiments, calculating additional parameter data further includes utilizing a database of specific surface areas for each of a set of minerals. The compute device, in some embodiments, may include circuitry configured to select one or more models as a function of the obtained parameter data. In some embodiments, the circuitry may be configured such that to select one or more models as a function of the obtained parameter data includes selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, the circuitry is configured such that producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. In some embodiments, the circuitry is configured such that producing at least one prediction includes reformatting the parameter data for use by the one or more models.|[0008] The circuitry may be configured such that producing at least one prediction includes utilizing one or more machine learning models. Additionally or alternatively, the circuitry may be configured utilize an ensemble of models to produce the at least one prediction. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period. The circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, the circuitry may be configured such that to produce at least one prediction involves producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured per hectare.|[0009] The circuitry may be configured to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, the circuitry is configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time. The circuitry may be configured such that to produce the at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions.|[0010] In some embodiments, the circuitry may be configured such that to produce at least one prediction involves determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. The compute device, in some embodiments, may have circuitry configured such that to produce at least one prediction involves determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. In some embodiments, the circuitry may be further configured to determine, from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, the circuitry is configured such that to present a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.|[0011] According to another aspect of the present disclosure, a method includes obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The method may further include producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. In doing so, the method may include simulating co-precipitation of iron with one or more toxic metals. The method may further include presenting, by the compute device, a visual representation of the at least one prediction in a user interface.|[0012] In some embodiments, producing, using one or more models from a library of models, at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. Producing, using one or more models from a library of models, at least one prediction may, in some embodiments, include utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, producing, using one or more models from a library of models, at least one prediction may include utilizing one or more models that simulate co-precipitation of iron with toxic metals. Obtaining parameter data may, in some embodiments, include obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, obtaining data indicative of properties of soil may include obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and a basalt mineral composition.|[0013] Obtaining parameter data may include obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. Obtaining parameter data as a function of an identification of the location where the carbon dioxide is to be captured may include reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. Obtaining parameter data may include obtaining parameter data through user input into corresponding fields of a user interface. The method may also include calculating, by the compute device and as a function of the obtained parameter data, additional parameter data for use by the one or more models. Calculating additional parameter data may include calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.|[0014] In some embodiments, calculating additional parameter data may additionally include utilizing a database of specific surface areas for each of a set of minerals. Producing at least one prediction may include selecting one or more models as a function of the obtained parameter data. Selecting one or more models as a function of the obtained parameter data may involve selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. Producing at least one prediction may include reformatting the parameter data for use by the one or more models. In some embodiments, producing at least one prediction involves utilizing one or more machine learning models. Producing at least one prediction may, in some embodiments, include utilizing an ensemble of models to produce the at least one prediction. Producing at least one prediction may include producing one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.|[0015] Producing one or more predictions may include producing one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, producing at least one prediction includes producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. Producing one or more predictions may, in some embodiments, include producing one or more predictions indicative of tons of carbon dioxide captured per hectare. In some embodiments, producing at least one prediction includes producing at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. Producing at least one prediction indicative of toxic metal concentrations in water may, in some embodiments, involve producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, producing at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time.|[0016] Producing the at least one prediction indicative of toxic metal concentrations in water may involve producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, producing the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions. Producing at least one prediction may include determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. In some embodiments, producing at least one prediction includes determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. The method may also include determining, by the compute device and from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, presenting a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.|[0017] According to another aspect of the present disclosure, one or more machine-readable storage media may include instructions stored thereon that, in response to being executed, cause a compute device to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The instructions may further cause the compute device to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Additionally, the instructions may cause the compute device to present a visual representation of the at least one prediction in a user interface. Further, the instructions may cause the compute device to perform any of the methods described above.|[0018] Additional features, which alone or in combination with any other feature(s), such as those listed above and/or those listed in the claims, may comprise patentable subject matter and will become apparent to those skilled in the art upon consideration of the following detailed description of various embodiments exemplifying the best mode of carrying out the embodiments as presently perceived.|(US20260017435)|BRIEF DESCRIPTION OF THE DRAWINGS|[0019] The concepts described herein are illustrated by way of example and not by way of limitation in the accompanying figures. For simplicity and clarity of illustration, elements illustrated in the figures are not necessarily drawn to scale. Where considered appropriate, reference labels have been repeated among the figures to indicate corresponding or analogous elements. The detailed description particularly refers to the accompanying figures in which:|[0020] FIG. 1 is a simplified block diagram of at least one embodiment of a system for modeling carbon dioxide removal through enhanced rock weathering;|[0021] FIG. 2 is a simplified block diagram of at least one embodiment of a compute device of the system of FIG. 1;|[0022] FIGS. 3-7 are flowcharts of at least one embodiment of a method for modeling carbon dioxide removal through enhanced rock weathering that may be performed by the system of FIG. 1;|[0023] FIGS. 8 and 9 are user interfaces that may be produced by the system of FIG. 1; and|[0024] FIG. 10 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating carbon capture as a function of years;|[0025] FIG. 11 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating a simulation of carbon capture as a function of time;|[0026] FIG. 12 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating the confidence interval of the simulations over a five year period;|[0027] FIG. 13 is one embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1; and|[0028] FIG. 14 is another embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1|(US20260017435)|DETAILED DESCRIPTION OF THE DRAWINGS|[0029] While the concepts of the present disclosure are susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and will be described herein in detail. It should be understood, however, that there is no intent to limit the concepts of the present disclosure to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives consistent with the present disclosure and the appended claims.|[0030] References in the specification to “one embodiment,” “an embodiment,” “an illustrative embodiment,” etc., indicate that the embodiment described may include a particular feature, structure, or characteristic, but every embodiment may or may not necessarily include that particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to effect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described. Additionally, it should be appreciated that items included in a list in the form of “at least one A, B, and C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C). Similarly, items listed in the form of “at least one of A, B, or C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C).|[0031] The disclosed embodiments may be implemented, in some cases, in hardware, firmware, software, or any combination thereof. The disclosed embodiments may also be implemented as instructions carried by or stored on a transitory or non-transitory machine-readable (e.g., computer-readable) storage medium, which may be read and executed by one or more processors. A machine-readable storage medium may be embodied as any storage device, mechanism, or other physical structure for storing or transmitting information in a form readable by a machine (e.g., a volatile or non-volatile memory, a media disc, or other media device).|[0032] In the drawings, some structural or method features may be shown in specific arrangements and/or orderings. However, it should be appreciated that such specific arrangements and/or orderings may not be required. Rather, in some embodiments, such features may be arranged in a different manner and/or order than shown in the illustrative figures. Additionally, the inclusion of a structural or method feature in a particular figure is not meant to imply that such feature is required in all embodiments and, in some embodiments, may not be included or may be combined with other features.|[0033] Referring now to FIG. 1, a system 100 for modeling carbon dioxide removal through enhanced rock weathering includes a set of one or more modeling compute devices 120, a set of source compute devices 140, 142, 144 and a set of target compute devices 150, 152, 154. In operation, the modeling compute devices 120 operate as a gateway 110 through which end users (e.g., scientists, organizations, etc.) of operating target compute devices 150, 152, 154 may view predictions (e.g., forecasts) of how much carbon dioxide will be captured in the soil at a particular location through a process of enhanced rock weathering. In enhanced rock weathering, rock, such as basalt, is added to soil at a location (e.g., one or more hectares of land) in a powdered form to increase the amount of carbon dioxide removed from the atmosphere through interaction between the carbon dioxide, water (e.g., rain), and rock. The composition of the basalt (e.g., mineral composition) as well as properties of the soil itself (e.g., porosity, carbon content, minerals, etc.) influence the amount of carbon dioxide that will be captured and may impact an amount of toxic metals present in the soil and/or water in the location as a result of the chemical processes involved in the capture of the carbon dioxide. As such, given the multitude of factors that can influence the amount of carbon dioxide removal, the modeling compute devices 120 may utilize a library of models 130 (e.g., thousands of models) and a database 132 of properties of minerals that also affect the amount of carbon dioxide that will be captured. The modeling compute devices 120 produce results 134, which may be embodied as data indicative of amount of carbon dioxide that will be captured under the specified conditions. Additionally, the results 134 may indicate the amount of toxic metals that are predicted to be present in the soil and water as a result of the chemical processes. Further, the results may be broken down across multiple years, depths, confidence intervals, or other parameters and may be the product of thousands of simulations using the set of models 130.|[0034] The source compute devices 140, 142, 144 may provide data indicative of properties of the soil in various locations, properties of basalt (e.g., various feed stocks of basalt), information indicative of a carbon credits market (e.g., an amount of carbon credits associated with an amount of carbon captured or removed from the atmosphere), data indicative of regulations associated with various locations (e.g., drinking water regulations, irrigation water regulations, soil regulations), and/or other data usable by the modeling compute devices 120 in simulating the capture of carbon from the atmosphere through enhanced rock weathering processes.|[0035] In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV). Further, the system 100 contributes to the trust that is necessary for the scale-up of climate-tech carbon dioxide removal (CDR) industries to the gigaton level. While the system 100, in some embodiments, focuses on enhanced rock weathering, the science and technologies can also be applied to storing carbon dioxide in basalt and sandstone aquifers and mine tailings.|[0036] A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring. The gateway 110, in the illustrative embodiment, is cloud-based, documented, and based on advanced cyberinfrastructure and data sciences that transform how modeling is delivered and how results are archived, analyzed, and presented. The gateway 110, in the illustrative embodiment, provides industry-standard authentication, authorization, and controlled sharing capabilities. Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.|[0037] In the illustrative embodiment, the gateway 110 may serve four types of clients: a) technical specialists at stakeholders (CDR and purchaser corporations, regulatory agencies, environmental groups) who can search a large library of models 130 to find the likely outcomes for their projects; b) geochemical experts who can develop or tweak their models 130 on the gateway 110, but aided by automatic documentation, archives, and traceability on the gateway; c) stakeholders with no in-house capabilities who wish to outsource the initial development of models 130 and run the models 130 on the gateway 110; d) stakeholders who need independent models as certification. The availability of the gateway 110 may operate to broaden the participation of underrepresented groups and less developed countries, helping achieve the common goal of implementing scalable solutions around the world.|[0038] Enhanced rock weathering can be generally represented with the equations shown below:|[0039] Other equations representative of geochemical reactions are set forth in “Environmental Applications of Geochemical Modeling” by Chen Zhu and Greg Anderson, published in 2002, the contents of which are incorporated herein by reference. As discussed herein, characteristics of the soil and basalt in the soil can significantly impact the amount of carbon dioxide that will be captured and the amounts of metals (e.g., toxic metals) that may be introduced into the soil and water through the enhanced rock wreathing process. The models 130, in the illustrative embodiment, account for the characteristics through parameters discussed herein. Further, the models 130 incorporate features that are not present in conventional modeling systems, including the following: a. Near-equilibrium rates (e.g., in systems with relatively low Gibbs energy) are modeled to be one to two orders of magnitude slower than the far-from-equilibrium rates (e.g., in systems with relatively high Gibbs energy), rather than the far-from-equilibrium rate constants used in other models; b. basalt weathering is simulated as irreversible reactions with unidirectional rates (not reversible reactions in other models, which are theoretically wrong); and c. the models 130 include co-precipitation of toxic metals released from enhanced rock weathering with iron oxyhydroxides. Without co-precipitation in the models 130, the forecasts of toxic metal released into soil may incorrectly indicate toxic metal amounts in excess of applicable regulations. The models 130 may be fine-tuned with time, and more components may be added to the model 130.|[0040] Further, the system 100, in the illustrative embodiment, provides a web-based model interface. Geochemical models are generally inaccessible to non-experts and the number of experts in the world is in short supply. The system 100 leverages expertise and experience of experts and makes modeling and modeling results available to non-experts. The gateway 110, in the illustrative embodiment, utilizes a database (e.g., the database 132) of mineralogical compositions of basalt feed stocks to be applied to croplands, and provides a web tool (e.g., a web based user interface) that allows users to input mineralogical compositions of the specific feed stock. Behind the web interface, the gateway 110 utilizes a database (e.g., the database 132) of different specific surface areas for different minerals. In operation, the gateway 110 may perform automatic input file generation (e.g., reformatting of parameter data into a format usable by the models 130).|[0041] The web interface and models enable users (e.g., operating the target compute devices 150, 152, 154) to combine different parameters and run different scenarios to view resulting predictions of carbon capture through enhanced rock weathering and side effects thereof. For example, users may compare how much carbon dioxide is captured by applying 100 tons of basalt per hectare versus ten tons of basalt per hectare, and using one feed stock of basalt (e.g., Oregon basalt) versus another feed stock of basalt (e.g., Columbia River basalt). Users may also view the differences in carbon capture given different particle sizes. Further, users may view data that is indicative of toxic metal release into water and soil under varying conditions.|[0042] In the illustrative embodiment, the gateway 110 may maintain a library of millions of simulations with a wide range of field conditions. The library may be searchable and the gateway 110 may enable users to locate modeling results and graphic presentations that fit their field conditions within minutes, rather than waiting for hours or longer for simulation results. The library may serve as a base for development or improvement of machine learning algorithms to (1) accelerate the simulations; and (2) find patterns, which lead to faster, more accurate, and more interpretable models. The models 130, in the illustrate embodiment, are calibrated geochemical models that bridge the gap between laboratory and field-based estimates of geochemical reactions. In particular, the models 130 may be calibrated with enhanced rock weathering batch scale laboratory experimental data, field data, and lysimeter experimental data. The results 134 may be embodied as databases and input files with adjusted parameters or semi-empirical scaling factors. In effect, the gateway 110 may provide independent, rigorous, models and modeling results that come with trust and creditability.|[0043] While a relatively small number of compute devices 120, 140, 142, 144, 150, 152, 154 are shown in FIG. 1 for simplicity and clarity, it should be understood that the number of compute devices, in practice, may range in the tens, hundreds, thousands, or more. Likewise, it should be understood that the compute devices 120, 140, 142, 144, 150, 152, 154 may be distributed differently or perform different roles than the configuration shown in FIG. 1. Further, though shown as separate compute devices 120, 140, 142, 144, 150, 152, 154 in some embodiments, the functionality of one or more of the compute devices 120, 140, 142, 144, 150, 152, 154 may be combined into fewer compute devices and/or distributed across more compute devices than those shown in FIG. 1.|[0044] Referring now to FIG. 2, an illustrative embodiment of a modeling compute device 120 includes a compute engine 210, an input/output (I/O) subsystem 216, communication circuitry 218, and one or more data storage devices 222. In some embodiments, the modeling compute device 120 may include one or more display devices 224 and/or one or more peripheral devices 226 (e.g., a mouse, a physical keyboard, etc.). In some embodiments, one or more of the illustrative components may be incorporated in, or otherwise form a portion of, another component. The compute engine 210 may be embodied as any type of device or collection of devices capable of performing various compute functions described below. In some embodiments, the compute engine 210 may be embodied as a single device such as an integrated circuit, an embedded system, a field-programmable gate array (FPGA), a system-on-a-chip (SOC), or other integrated system or device. Additionally, in the illustrative embodiment, the compute engine 210 includes or is embodied as a processor 212 and a memory 214. The processor 212 may be embodied as any type of processor capable of performing the functions described herein. For example, the processor 212 may be embodied as a single or multi-core processor(s), a microcontroller, or other processor or processing/controlling circuit. In some embodiments, the processor 212 may be embodied as, include, or be coupled to an FPGA, an application specific integrated circuit (ASIC), reconfigurable hardware or hardware circuitry, or other specialized hardware to facilitate performance of the functions described herein.|[0045] In embodiments, the processor 212 is capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, a set of instructions which when executed by the processor 212 cause the modeling compute device 120 to perform one or more operations described herein. In embodiments, the processor 212 is further capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, one or more signals from external sources, e.g., from the peripheral devices 226 or via the communication circuitry 218 from an external compute device, external source, or external network. As one will appreciate, a signal may contain encoded instructions and/or information. In embodiments, once received, such a signal may first be stored, e.g., in the memory 214 or in the data storage device(s) 222, thereby allowing for a time delay in the receipt by the processor 212 before the processor 212 operates on a received signal. Likewise, the processor 212 may generate one or more output signals, which may be transmitted to an external device, e.g., an external memory or an external compute engine via the communication circuitry 218 or, e.g., to one or more display devices 224. In some embodiments, a signal may be subjected to a time shift in order to delay the signal. For example, a signal may be stored on one or more storage devices 222 to allow for a time shift prior to transmitting the signal to an external device. One will appreciate that the form of a particular signal will be determined by the particular encoding a signal is subject to at any point in its transmission (e.g., a signal stored will have a different encoding than a signal in transit, or, e.g., an analog signal will differ in form from a digital version of the signal prior to an analog-to-digital (A/D) conversion).|[0046] The main memory 214 may be embodied as any type of volatile (e.g., dynamic random access memory (DRAM), etc.) or non-volatile memory or data storage capable of performing the functions described herein. Volatile memory may be a storage medium that requires power to maintain the state of data stored by the medium. In some embodiments, all or a portion of the main memory 214 may be integrated into the processor 212. In operation, the main memory 214 may store various software and data used during operation such as models, databases, simulation results, applications, libraries, and drivers.|[0047] The compute engine 210 is communicatively coupled to other components of the modeling compute device 120 via the I/O subsystem 216, which may be embodied as circuitry and/or components to facilitate input/output operations with the compute engine 210 (e.g., with the processor 212 and the main memory 214) and other components of the modeling compute device 120. For example, the I/O subsystem 216 may be embodied as, or otherwise include, memory controller hubs, input/output control hubs, integrated sensor hubs, firmware devices, communication links (e.g., point-to-point links, bus links, wires, cables, light guides, printed circuit board traces, etc.), and/or other components and subsystems to facilitate the input/output operations. In some embodiments, the I/O subsystem 216 may form a portion of a system-on-a-chip (SoC) and be incorporated, along with one or more of the processor 212, the main memory 214, and other components of the modeling compute device 120, into the compute engine 210.|[0048] The communication circuitry 218 may be embodied as any communication circuit, device, or collection thereof, capable of enabling communications over a network between the modeling compute device 120 and another device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). The communication circuitry 218 may be configured to use any one or more communication technology (e.g., wired or wireless communications) and associated protocols (e.g., Ethernet, Wi-Fi®, WiMAX, Bluetooth®, etc.) to effect such communication.|[0049] The illustrative communication circuitry 218 includes a network interface controller (NIC) 220. The NIC 220 may be embodied as one or more add-in-boards, daughter cards, network interface cards, controller chips, chipsets, or other devices that may be used by the modeling compute device 120 to connect with another compute device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). In some embodiments, the NIC 220 may be embodied as part of a system-on-a-chip (SoC) that includes one or more processors, or included on a multichip package that also contains one or more processors. In some embodiments, the NIC 220 may include a local processor (not shown) and/or a local memory (not shown) that are both local to the NIC 220. Additionally or alternatively, in such embodiments, the local memory of the NIC 220 may be integrated into one or more components of the modeling compute device 120 at the board level, socket level, chip level, and/or other levels.|[0050] Each data storage device 222, may be embodied as any type of device configured for short-term or long-term storage of data such as, for example, memory devices and circuits, memory cards, hard disk drives, solid-state drives, or other data storage device. Each data storage device 222 may include a system partition that stores data and firmware code for the data storage device 222 and one or more operating system partitions that store data files and executables for operating systems.|[0051] Each display device 224 may be embodied as any device or circuitry (e.g., a liquid crystal display (LCD), a light emitting diode (LED) display, a cathode ray tube (CRT) display, etc.) configured to display visual information (e.g., text, graphics, etc.) to a user. In some embodiments, a display device 224 may be embodied as a touch screen (e.g., a screen incorporating resistive touchscreen sensors, capacitive touchscreen sensors, surface acoustic wave (SAW) touchscreen sensors, infrared touchscreen sensors, optical imaging touchscreen sensors, acoustic touchscreen sensors, and/or other type of touchscreen sensors) to detect selections of on-screen user interface elements or gestures from a user.|[0052] In the illustrative embodiment, the components of the modeling compute device 120 are housed in a single unit. However, in other embodiments, the components may be in separate housings, in separate racks of a data center, and/or spread across multiple data centers or other facilities. The compute devices 140, 142, 144, 150, 152, 154 may have components similar to those described in FIG. 2 with reference to the modeling compute device 120. The description of those components of the modeling compute device 120 is equally applicable to the description of components of the compute devices 140, 142, 144, 150, 152, 154. Further, it should be appreciated that any of the devices 120, 140, 142, 144, 150, 152, 154 may include other components, sub-components, and devices commonly found in a computing device, which are not discussed above in reference to the modeling compute device 120 and not discussed herein for clarity of the description.|[0053] In the illustrative embodiment, the compute devices 120, 140, 142, 144, 150, 152, 154 are in communication via a network 160, which may be embodied as any type of wired or wireless communication network, including global networks (e.g., the internet), wide area networks (WANs), local area networks (LANs), digital subscriber line (DSL) networks, cable networks (e.g., coaxial networks, fiber networks, etc.), cellular networks (e.g., Global System for Mobile Communications (GSM), Long Term Evolution (LTE), Worldwide Interoperability for Microwave Access (WiMAX), 3G, 4G, 5G, etc.), a radio area network (RAN), or any combination thereof.|[0054] Referring now to FIG. 3, the system 100 (e.g., a modeling compute device 120 of the gateway 110) may perform a method 300 for modeling carbon dioxide removal through enhanced rock weathering. The method 300, in the illustrative embodiment, begins with block 302 in which the modeling compute device 120 obtains parameter data indicative of parameters for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering (e.g., the application of basalt dust to soil to increase the amount of carbon dioxide captured through the interaction of water (e.g., rain), carbon dioxide, and rock (e.g., the basalt dust)). In doing so, and as indicated in block 304, the modeling compute device 120 obtains data indicative of properties of soil in a location where the carbon dioxide is to be captured (e.g., removed from the atmosphere through enhanced rock weathering). In the illustrative embodiment, the modeling compute device 120 may obtain data indicative of minerals in the soil (e.g., a numeric value, such as a number indicative of a percentage of the soil comprising minerals), as indicated in block 306. As indicated in block 308, the modeling compute device 120 may obtain data indicative of carbon in the soil (e.g., a numeric value indicative of a percentage of the soil comprising carbon).|[0055] The modeling compute device 120 may additionally obtain data indicative of effective porosity of the soil where the carbon is to be captured, as indicated in block 310. The effective porosity may be expressed, in at least some embodiments, as a numeric value (e.g., a percentage). As indicated in block 312, the modeling compute device 120 may obtain parameter data indicative of total specific surface area. In at least some embodiments, the total specific surface area may be expressed as square meters per gram. The modeling compute device 120 may obtain data indicative of the height of a top soil layer, as indicated in block 314. The height, in the illustrative embodiment, is expressed in meters. Further, the modeling compute device 120 may obtain data indicative of an amount of basalt added to the soil (e.g., tons per hectare), as indicated in block 316. Further, the modeling compute device 120 may obtain data indicative of basalt density, such as in grams per cubic centimeter, as indicated in block 318. Additionally, the modeling compute device 120 may obtain data indicative of bulk soil density, as indicated in block 320. The bulk soil density, in at least some embodiments, may be expressed as grams per cubic centimeter. The modeling compute device 120 may also obtain data indicative of basalt mineral composition, as indicated in block 322. The mineral composition of the basalt may be structured as one or more pairs of values, with each pair including an identifier (e.g., name, abbreviation, etc.) of a mineral and a corresponding percentage (e.g., indicative of a percentage of the basalt feed stock that the mineral constitutes).|[0056] Still referring to FIG. 3, the modeling compute device 120 may obtain the parameter data as a function of (e.g., based on) an identification of the location where the carbon dioxide is to be captured in the soil, as indicated in block 324. In doing so, the modeling compute device 120 may read parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of properties of soil associated with location identifiers (e.g., plot numbers, geographic coordinates, zip codes, etc.), as indicated in block 326. In some embodiments, the modeling compute device 120 may obtain parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of mineral compositions from each of multiple basalt feed stocks, as indicated in block 328. Additionally or alternatively, the modeling compute device 120 may obtain parameter data through user input into corresponding fields (e.g., text boxes, check boxes, etc.) of a user interface (e.g., a graphical user interface presented by a target compute device 150, 152, 154 based on code (e.g., hypertext markup language (HTML) and/or JavaScript) and images (e.g., portable network graphics (PNG) files, Joint Photographic Experts Group (JPEG) files, or the like) transmitted from the modeling compute device 120 to the target compute device(s) 150, 152, 154 via the network 160, as indicated in block 330. An embodiment of a user interface 800 with which the modeling compute device 120 may obtain parameter data is shown in FIG. 8. The user interface 800 includes a first screen 810 that comprises parameter data about soil properties and a second screen 820 that includes parameter data about basalt mineral makeup. The user interface 800 provides one embodiment that users can use to input parameters related to soil properties and basalt mineral composition, run the models, and calculate how much CO2 can be sequestered.|[0057] Referring now to FIG. 4, the method 300 continues in block 332 in which the modeling compute device 120 may calculate, as a function of the obtained parameter data, additional parameter data for use by one or more models (e.g., the models 130). In doing so, the modeling compute device 120 may calculate air and blind pores (e.g., a numeric value), as indicated in block 334. The modeling compute device 120 may additionally calculate a volume of soil per hectare, as indicated in block 336. Further, the modeling compute device 120 may calculate a number of volume (e.g., liters) of pore water per unit of area (e.g., hectare), as indicated in block 338. Additionally, the modeling compute device 120 may calculate a mass of basalt per unit of volume of the soil, as indicated in block 340. In addition, the modeling compute device 120 may calculate a concentration of basalt in the soil, as indicated in block 342. Further, the modeling compute device 120 may calculate a total weight percentage, as indicated in block 344. The modeling compute device 120 may also calculate a rock specific surface area, as indicated in block 346. In addition, the modeling compute device 120 may calculate a total surface area, in block 348. In performing the calculations, the modeling compute device 120 may utilize a database (e.g., a database 132) of specific surface areas for each of a set of minerals (e.g., minerals in the soil, in the basalt, etc.), as indicated in block 350. An embodiment of a user interface 900 in which the modeling compute device 120 may display additional parameters calculated as discussed above is shown in FIG. 9. In some embodiments, the user interface 800 includes a third screen 830 that may display additional parameters calculated as discussed above.|[0058] After obtaining the parameter data, the method 300, in the illustrative embodiment, advances to block 352, in which the modeling compute device 120 produces, using one or models from a library of models (e.g., the models 130), one or more predictions indicative of an amount of carbon dioxide that will be removed from the atmosphere (e.g., captured through enhanced rock weathering). In doing so, the modeling compute device 120 may select one or more models 130 as a function of the obtained parameter data, as indicated in block 354. That is, the modeling compute device 120 may select one or more models 130 from the library of models as a function of a determined similarity (e.g., a similarity score, such as a calculated distance (e.g., a Euclidean distance, a cosine similarity, a result of a clustering analysis, etc.)) of the parameter data (e.g., obtained in block 302) to reference parameters for which one or more corresponding models 130 have been identified (e.g., in a data set in the memory 214 or storage 222, in a database 132, etc.) as having a high accuracy of predictions (e.g., the results 134 produced by those models have been shown to predict within a predefined threshold of accuracy (e.g., a defined percentage), actual results that were later measured in field tests). That is, if a particular model 130 is identified as more accurately predicting the amount of carbon dioxide that will be removed from the atmosphere than other models, when the parameters are similar to those obtained in block 302, the modeling compute device 120 may select that model for use.|[0059] In some embodiments, as indicated in block 358, the modeling compute device 120 may select one or more models 130 as a function of a distance of the location where the carbon dioxide is to be captured to each of a set of reference locations associated with the models 130. That is, a data set (e.g., in the memory 214, the data storage 222, or a database 132) may identify a location (e.g., a zip code, a set of geographic coordinates, or other identifier of a location) with each model 130 in the library (e.g., because the corresponding model 130 has been shown to produce predictions with high accuracy for the associated location) and the modeling compute device 120 may select a set (e.g., one or more) of the models 130 that are closest to the location where the carbon dioxide is to be captured.|[0060] Referring now to FIG. 5, in block 360, the modeling compute device 120 may reformat the parameter data for use by the models 130 (e.g., by converting the data into a file format that the models 130 are configured to parse (e.g., using a scripting language such as Python)). As indicated in block 362, the modeling compute device 120 may select one or more machine learning models (e.g., models, such as neural networks, decision trees, or others that may iteratively improve in prediction accuracy based on feedback). In some embodiments, the modeling compute device 120 may select an ensemble (e.g., a combination of models, in which outputs of the individual models may be weighted relative to each other), as indicated in block 364. The models 130 may include one or more models implemented by PHREEQC (e.g., PHREEQC 3), from the U.S. Geological Survey, GEM (e.g., reservoir modeling), TOUGHREACT from Lawrence Berkeley National Laboratory, and/or other models (e.g., provided by entities associated with one or more of the source compute devices 140, 142, 144). The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period, as indicated in block 366. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured each year of a defined number of years at the specified location, as indicated in block 368.|[0061] The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per unit of area, as indicated in block 370. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per hectare, as indicated in block 372. In the illustrative embodiment, and unlike conventional systems, the modeling compute device 120 utilizes models that simulate co-precipitation of iron with toxic metals, as indicated in block 374. Additionally, and unlike conventional systems, the modeling compute device 120, in the illustrative embodiment, utilizes models that simulate basalt weathering as irreversible reactions with unidirectional rates, as indicated in block 376. Further, and unlike conventional systems, the modeling compute device 120 in the illustrative embodiment utilizes models in which near-equilibrium (e.g., within a defined percentage of an equilibrium state) rates are one to two orders of magnitude slower than far-from-equilibrium (e.g., not within the defined percentage of the equilibrium state) rates, as indicated in block 378. Further, and as indicated in block 380, the modeling compute device 120, in the illustrative embodiment, produces one or more predictions indicative of toxic metal concentrations in water associated with the location where the carbon dioxide is to be captured. In doing so, the modeling compute device 120 may produce one or more predictions indicative of concentrations of Nickel, Chromium, and/or Cadmium in the water, as indicated in block 382.|[0062] Referring now to FIG. 6, the modeling compute device 120 may produce the one or more predications as a function of depth (e.g., depth of the water), as indicated in block 384. As indicated in block 386, the modeling compute device 120 may produce the one or more predictions regarding toxic metals in the water as a function of time (e.g., amount of toxic metals in the water per year). In some embodiments, the modeling compute device 120 may produce the predictions of toxic metals in the water relative to one or more regulations associated with the location where the carbon dioxide is to be captured, as indicated in block 388. That is, the modeling compute device 120 may obtain data (e.g., from a database 132, from a source compute device 140, 142, 144) indicative of applicable regulations and indicate whether the predicted amount of toxic metals satisfies (e.g., does not violate the regulation(s), is close to (e.g., within a defined percentage of), etc.) a limit specified by the regulations. The modeling compute device 120 may produce the prediction(s) relative to drinking water regulations and/or irrigation water regulations, as indicated in blocks 390, 392. The modeling compute device 120 may produce one or more predictions indicative of toxic metal concentrations in the soil associated with the location where the carbon dioxide is to be captured, as indicated in block 394. In doing so, the modeling compute device 120 may produce prediction(s) indicative of concentrations of Nickel, Chromium, and/or Cadmium in the soil, as indicated in block 396. The modeling compute device 120 may produce the prediction(s) as a function of depth (e.g., in the soil) and/or as a function of time, as indicated in blocks 398, 400. Similar to block 388, the modeling compute device 120 may produce the prediction(s) of toxic metals in the soil relative to one or more regulations associated with the location, as indicated in block 402.|[0063] Referring now to FIG. 7, the modeling compute device 120 may produce data indicative of probabilities (e.g., confidence) associated with the one or more predictions, as indicated in block 404. For example, the modeling compute device 120 may produce a predictions as confidence intervals, with one prediction associated with a particular level of confidence (e.g., a percentage of likelihood), and one or more other predictions associated with other levels of confidence. As indicated in block 406, the modeling compute device 120 may determine an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. For example, the modeling compute device 120 may obtain data (e.g., from a source compute device 140, 142, 144, a database 132, etc.) indicative of a conversion rate between tons of carbon captured and a number of corresponding carbon credits and multiply the predicted amount of carbon dioxide by the conversion rate to determine the amount of carbon credits. In some embodiments, the modeling compute device 120 may adjust the number of carbon credits based on a probability or confidence level associated with the predicted amount of carbon dioxide to be removed from block 404 (e.g., by multiplying the amount of carbon dioxide by a percentage associated with the probability or confidence level). As indicated in block 408, the modeling compute device 120 may determine soil parameters that will increase capture of carbon dioxide at the location. For example, and as indicated in block 410, the modeling compute device 120 may determine, from a set of multiple basalt feed stocks, each having different mineral compositions and/or other properties, a basalt feed stock predicted to capture the most carbon dioxide in the location while maintaining compliance with regulations (e.g., toxic metals in the soil, toxic metals in the water). The modeling compute device 120 may do so by simulating carbon dioxide capture with each of the basalt feed stocks using the models 130 and identifying the basalt feed stock that satisfies the above conditions to the greatest degree.|[0064] Continuing the method 300, the modeling compute device 120 may present a visual representation of the one or more prediction(s) in a user interface, as indicated in block 412. In the illustrative embodiment, the modeling compute device 120 produces visual presentation(s) of the prediction(s) in a web based interface (e.g., based on a HTML, JavaScript, and image data sent from the modeling compute device 120 to one or more rending engines (e.g., web browser(s)) executed by corresponding target compute devices 150, 152, 154). As indicated in block 416, in producing one or more visual representations of the prediction(s), the modeling compute device 120 may present visual representations that include interactive graphs (e.g., in which time periods, depths, or other parameters may be selected and a corresponding graph is presented). Example embodiments of visual representations 1000, 1100, 1200, 1300, 1400 of the predictions that may be presented by the modeling compute device 120 and displayed by one or more of the corresponding target compute devices 150, 152, 154 are shown in FIGS. 10-14.|[0065] While certain illustrative embodiments have been described in detail in the drawings and the foregoing description, such an illustration and description is to be considered as exemplary and not restrictive in character, it being understood that only illustrative embodiments have been shown and described and that all changes and modifications that come within the spirit of the disclosure are desired to be protected. There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein. It will be noted that alternative embodiments of the apparatus, systems, and methods of the present disclosure may not include all of the features described, yet still benefit from at least some of the advantages of such features. Those of ordinary skill in the art may readily devise their own implementations of the apparatus, systems, and methods that incorporate one or more of the features of the present disclosure. (US20260017435)|CROSS-REFERENCE TO RELATED APPLICATIONS|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/669,351 filed on Jul. 10, 2024, the disclosure of which is expressly incorporated herein.|(US20260017435)|BACKGROUND|[0002] Climate change is a growing concern across the world as atmospheric greenhouse gases such as carbon dioxide trap energy radiated from the sun. While a direct result of increases in greenhouse gases is increased temperatures on Earth, knock on effects include droughts, flooding, loss of biodiversity, and disruptions in energy and transportation systems across the world. Through interactions between water and rock (e.g., in soil), carbon dioxide can be captured (e.g., removed) from the atmosphere and correspondingly lessen the effects of climate change. However, given the multitude of factors that influence the complex interactions between water and rock, it is not feasible in conventional computerized systems to reliably determine the amount of carbon dioxide that will be removed in a given location, under a given set of conditions, or to predict side effects of any efforts to enhance the capture of carbon dioxide in the soil. Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.|SUMMARY|[0003] The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:|[0004] According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may be further configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. Producing a prediction may include simulating co-precipitation of iron with one or more toxic metals. The circuitry may be further configured to present a visual representation of the at least one prediction in a user interface.|[0005] In some embodiments, the circuitry may be configured such that using one or more models from a library of models to produce at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. The circuitry may also be configured to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, the circuitry may be configured to utilize one or more models that simulate co-precipitation of iron with toxic metals. The circuitry may be configured to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that obtaining data indicative of properties of soil includes obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and basalt mineral composition.|[0006] The circuitry may be configured such that obtaining parameter data includes obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured to obtain parameter data as a function of an identification of the location where the carbon dioxide is to be captured by reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. The circuitry may be configured to obtain parameter data through user input into corresponding fields of a user interface. In some embodiments, the circuitry may be further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models. The circuitry may be configured such that calculating additional parameter data involves calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.|[0007] In some embodiments, calculating additional parameter data further includes utilizing a database of specific surface areas for each of a set of minerals. The compute device, in some embodiments, may include circuitry configured to select one or more models as a function of the obtained parameter data. In some embodiments, the circuitry may be configured such that to select one or more models as a function of the obtained parameter data includes selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, the circuitry is configured such that producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. In some embodiments, the circuitry is configured such that producing at least one prediction includes reformatting the parameter data for use by the one or more models.|[0008] The circuitry may be configured such that producing at least one prediction includes utilizing one or more machine learning models. Additionally or alternatively, the circuitry may be configured utilize an ensemble of models to produce the at least one prediction. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period. The circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, the circuitry may be configured such that to produce at least one prediction involves producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured per hectare.|[0009] The circuitry may be configured to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, the circuitry is configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time. The circuitry may be configured such that to produce the at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions.|[0010] In some embodiments, the circuitry may be configured such that to produce at least one prediction involves determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. The compute device, in some embodiments, may have circuitry configured such that to produce at least one prediction involves determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. In some embodiments, the circuitry may be further configured to determine, from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, the circuitry is configured such that to present a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.|[0011] According to another aspect of the present disclosure, a method includes obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The method may further include producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. In doing so, the method may include simulating co-precipitation of iron with one or more toxic metals. The method may further include presenting, by the compute device, a visual representation of the at least one prediction in a user interface.|[0012] In some embodiments, producing, using one or more models from a library of models, at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. Producing, using one or more models from a library of models, at least one prediction may, in some embodiments, include utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, producing, using one or more models from a library of models, at least one prediction may include utilizing one or more models that simulate co-precipitation of iron with toxic metals. Obtaining parameter data may, in some embodiments, include obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, obtaining data indicative of properties of soil may include obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and a basalt mineral composition.|[0013] Obtaining parameter data may include obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. Obtaining parameter data as a function of an identification of the location where the carbon dioxide is to be captured may include reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. Obtaining parameter data may include obtaining parameter data through user input into corresponding fields of a user interface. The method may also include calculating, by the compute device and as a function of the obtained parameter data, additional parameter data for use by the one or more models. Calculating additional parameter data may include calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.|[0014] In some embodiments, calculating additional parameter data may additionally include utilizing a database of specific surface areas for each of a set of minerals. Producing at least one prediction may include selecting one or more models as a function of the obtained parameter data. Selecting one or more models as a function of the obtained parameter data may involve selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. Producing at least one prediction may include reformatting the parameter data for use by the one or more models. In some embodiments, producing at least one prediction involves utilizing one or more machine learning models. Producing at least one prediction may, in some embodiments, include utilizing an ensemble of models to produce the at least one prediction. Producing at least one prediction may include producing one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.|[0015] Producing one or more predictions may include producing one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, producing at least one prediction includes producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. Producing one or more predictions may, in some embodiments, include producing one or more predictions indicative of tons of carbon dioxide captured per hectare. In some embodiments, producing at least one prediction includes producing at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. Producing at least one prediction indicative of toxic metal concentrations in water may, in some embodiments, involve producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, producing at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time.|[0016] Producing the at least one prediction indicative of toxic metal concentrations in water may involve producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, producing the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions. Producing at least one prediction may include determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. In some embodiments, producing at least one prediction includes determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. The method may also include determining, by the compute device and from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, presenting a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.|[0017] According to another aspect of the present disclosure, one or more machine-readable storage media may include instructions stored thereon that, in response to being executed, cause a compute device to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The instructions may further cause the compute device to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Additionally, the instructions may cause the compute device to present a visual representation of the at least one prediction in a user interface. Further, the instructions may cause the compute device to perform any of the methods described above.|[0018] Additional features, which alone or in combination with any other feature(s), such as those listed above and/or those listed in the claims, may comprise patentable subject matter and will become apparent to those skilled in the art upon consideration of the following detailed description of various embodiments exemplifying the best mode of carrying out the embodiments as presently perceived.|(US20260017435)|BRIEF DESCRIPTION OF THE DRAWINGS|[0019] The concepts described herein are illustrated by way of example and not by way of limitation in the accompanying figures. For simplicity and clarity of illustration, elements illustrated in the figures are not necessarily drawn to scale. Where considered appropriate, reference labels have been repeated among the figures to indicate corresponding or analogous elements. The detailed description particularly refers to the accompanying figures in which:|[0020] FIG. 1 is a simplified block diagram of at least one embodiment of a system for modeling carbon dioxide removal through enhanced rock weathering;|[0021] FIG. 2 is a simplified block diagram of at least one embodiment of a compute device of the system of FIG. 1;|[0022] FIGS. 3-7 are flowcharts of at least one embodiment of a method for modeling carbon dioxide removal through enhanced rock weathering that may be performed by the system of FIG. 1;|[0023] FIGS. 8 and 9 are user interfaces that may be produced by the system of FIG. 1; and|[0024] FIG. 10 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating carbon capture as a function of years;|[0025] FIG. 11 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating a simulation of carbon capture as a function of time;|[0026] FIG. 12 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating the confidence interval of the simulations over a five year period;|[0027] FIG. 13 is one embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1; and|[0028] FIG. 14 is another embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1;|(US20260017435)|DETAILED DESCRIPTION OF THE DRAWINGS|[0029] While the concepts of the present disclosure are susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and will be described herein in detail. It should be understood, however, that there is no intent to limit the concepts of the present disclosure to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives consistent with the present disclosure and the appended claims.|[0030] References in the specification to “one embodiment,” “an embodiment,” “an illustrative embodiment,” etc., indicate that the embodiment described may include a particular feature, structure, or characteristic, but every embodiment may or may not necessarily include that particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to effect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described. Additionally, it should be appreciated that items included in a list in the form of “at least one A, B, and C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C). Similarly, items listed in the form of “at least one of A, B, or C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C).|[0031] The disclosed embodiments may be implemented, in some cases, in hardware, firmware, software, or any combination thereof. The disclosed embodiments may also be implemented as instructions carried by or stored on a transitory or non-transitory machine-readable (e.g., computer-readable) storage medium, which may be read and executed by one or more processors. A machine-readable storage medium may be embodied as any storage device, mechanism, or other physical structure for storing or transmitting information in a form readable by a machine (e.g., a volatile or non-volatile memory, a media disc, or other media device).|[0032] In the drawings, some structural or method features may be shown in specific arrangements and/or orderings. However, it should be appreciated that such specific arrangements and/or orderings may not be required. Rather, in some embodiments, such features may be arranged in a different manner and/or order than shown in the illustrative figures. Additionally, the inclusion of a structural or method feature in a particular figure is not meant to imply that such feature is required in all embodiments and, in some embodiments, may not be included or may be combined with other features.|[0033] Referring now to FIG. 1, a system 100 for modeling carbon dioxide removal through enhanced rock weathering includes a set of one or more modeling compute devices 120, a set of source compute devices 140, 142, 144 and a set of target compute devices 150, 152, 154. In operation, the modeling compute devices 120 operate as a gateway 110 through which end users (e.g., scientists, organizations, etc.) of operating target compute devices 150, 152, 154 may view predictions (e.g., forecasts) of how much carbon dioxide will be captured in the soil at a particular location through a process of enhanced rock weathering. In enhanced rock weathering, rock, such as basalt, is added to soil at a location (e.g., one or more hectares of land) in a powdered form to increase the amount of carbon dioxide removed from the atmosphere through interaction between the carbon dioxide, water (e.g., rain), and rock. The composition of the basalt (e.g., mineral composition) as well as properties of the soil itself (e.g., porosity, carbon content, minerals, etc.) influence the amount of carbon dioxide that will be captured and may impact an amount of toxic metals present in the soil and/or water in the location as a result of the chemical processes involved in the capture of the carbon dioxide. As such, given the multitude of factors that can influence the amount of carbon dioxide removal, the modeling compute devices 120 may utilize a library of models 130 (e.g., thousands of models) and a database 132 of properties of minerals that also affect the amount of carbon dioxide that will be captured. The modeling compute devices 120 produce results 134, which may be embodied as data indicative of amount of carbon dioxide that will be captured under the specified conditions. Additionally, the results 134 may indicate the amount of toxic metals that are predicted to be present in the soil and water as a result of the chemical processes. Further, the results may be broken down across multiple years, depths, confidence intervals, or other parameters and may be the product of thousands of simulations using the set of models 130.|[0034] The source compute devices 140, 142, 144 may provide data indicative of properties of the soil in various locations, properties of basalt (e.g., various feed stocks of basalt), information indicative of a carbon credits market (e.g., an amount of carbon credits associated with an amount of carbon captured or removed from the atmosphere), data indicative of regulations associated with various locations (e.g., drinking water regulations, irrigation water regulations, soil regulations), and/or other data usable by the modeling compute devices 120 in simulating the capture of carbon from the atmosphere through enhanced rock weathering processes.|[0035] In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV). Further, the system 100 contributes to the trust that is necessary for the scale-up of climate-tech carbon dioxide removal (CDR) industries to the gigaton level. While the system 100, in some embodiments, focuses on enhanced rock weathering, the science and technologies can also be applied to storing carbon dioxide in basalt and sandstone aquifers and mine tailings.|[0036] A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring. The gateway 110, in the illustrative embodiment, is cloud-based, documented, and based on advanced cyberinfrastructure and data sciences that transform how modeling is delivered and how results are archived, analyzed, and presented. The gateway 110, in the illustrative embodiment, provides industry-standard authentication, authorization, and controlled sharing capabilities. Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.|[0037] In the illustrative embodiment, the gateway 110 may serve four types of clients: a) technical specialists at stakeholders (CDR and purchaser corporations, regulatory agencies, environmental groups) who can search a large library of models 130 to find the likely outcomes for their projects; b) geochemical experts who can develop or tweak their models 130 on the gateway 110, but aided by automatic documentation, archives, and traceability on the gateway; c) stakeholders with no in-house capabilities who wish to outsource the initial development of models 130 and run the models 130 on the gateway 110; d) stakeholders who need independent models as certification. The availability of the gateway 110 may operate to broaden the participation of underrepresented groups and less developed countries, helping achieve the common goal of implementing scalable solutions around the world.|[0038] Enhanced rock weathering can be generally represented with the equations shown below:|[0039] Other equations representative of geochemical reactions are set forth in “Environmental Applications of Geochemical Modeling” by Chen Zhu and Greg Anderson, published in 2002, the contents of which are incorporated herein by reference. As discussed herein, characteristics of the soil and basalt in the soil can significantly impact the amount of carbon dioxide that will be captured and the amounts of metals (e.g., toxic metals) that may be introduced into the soil and water through the enhanced rock wreathing process. The models 130, in the illustrative embodiment, account for the characteristics through parameters discussed herein. Further, the models 130 incorporate features that are not present in conventional modeling systems, including the following: a. Near-equilibrium rates (e.g., in systems with relatively low Gibbs energy) are modeled to be one to two orders of magnitude slower than the far-from-equilibrium rates (e.g., in systems with relatively high Gibbs energy), rather than the far-from-equilibrium rate constants used in other models; b. basalt weathering is simulated as irreversible reactions with unidirectional rates (not reversible reactions in other models, which are theoretically wrong); and c. the models 130 include co-precipitation of toxic metals released from enhanced rock weathering with iron oxyhydroxides. Without co-precipitation in the models 130, the forecasts of toxic metal released into soil may incorrectly indicate toxic metal amounts in excess of applicable regulations. The models 130 may be fine-tuned with time, and more components may be added to the model 130.|[0040] Further, the system 100, in the illustrative embodiment, provides a web-based model interface. Geochemical models are generally inaccessible to non-experts and the number of experts in the world is in short supply. The system 100 leverages expertise and experience of experts and makes modeling and modeling results available to non-experts. The gateway 110, in the illustrative embodiment, utilizes a database (e.g., the database 132) of mineralogical compositions of basalt feed stocks to be applied to croplands, and provides a web tool (e.g., a web based user interface) that allows users to input mineralogical compositions of the specific feed stock. Behind the web interface, the gateway 110 utilizes a database (e.g., the database 132) of different specific surface areas for different minerals. In operation, the gateway 110 may perform automatic input file generation (e.g., reformatting of parameter data into a format usable by the models 130).|[0041] The web interface and models enable users (e.g., operating the target compute devices 150, 152, 154) to combine different parameters and run different scenarios to view resulting predictions of carbon capture through enhanced rock weathering and side effects thereof. For example, users may compare how much carbon dioxide is captured by applying 100 tons of basalt per hectare versus ten tons of basalt per hectare, and using one feed stock of basalt (e.g., Oregon basalt) versus another feed stock of basalt (e.g., Columbia River basalt). Users may also view the differences in carbon capture given different particle sizes. Further, users may view data that is indicative of toxic metal release into water and soil under varying conditions.|[0042] In the illustrative embodiment, the gateway 110 may maintain a library of millions of simulations with a wide range of field conditions. The library may be searchable and the gateway 110 may enable users to locate modeling results and graphic presentations that fit their field conditions within minutes, rather than waiting for hours or longer for simulation results. The library may serve as a base for development or improvement of machine learning algorithms to (1) accelerate the simulations; and (2) find patterns, which lead to faster, more accurate, and more interpretable models. The models 130, in the illustrate embodiment, are calibrated geochemical models that bridge the gap between laboratory and field-based estimates of geochemical reactions. In particular, the models 130 may be calibrated with enhanced rock weathering batch scale laboratory experimental data, field data, and lysimeter experimental data. The results 134 may be embodied as databases and input files with adjusted parameters or semi-empirical scaling factors. In effect, the gateway 110 may provide independent, rigorous, models and modeling results that come with trust and creditability.|[0043] While a relatively small number of compute devices 120, 140, 142, 144, 150, 152, 154 are shown in FIG. 1 for simplicity and clarity, it should be understood that the number of compute devices, in practice, may range in the tens, hundreds, thousands, or more. Likewise, it should be understood that the compute devices 120, 140, 142, 144, 150, 152, 154 may be distributed differently or perform different roles than the configuration shown in FIG. 1. Further, though shown as separate compute devices 120, 140, 142, 144, 150, 152, 154 in some embodiments, the functionality of one or more of the compute devices 120, 140, 142, 144, 150, 152, 154 may be combined into fewer compute devices and/or distributed across more compute devices than those shown in FIG. 1.|[0044] Referring now to FIG. 2, an illustrative embodiment of a modeling compute device 120 includes a compute engine 210, an input/output (I/O) subsystem 216, communication circuitry 218, and one or more data storage devices 222. In some embodiments, the modeling compute device 120 may include one or more display devices 224 and/or one or more peripheral devices 226 (e.g., a mouse, a physical keyboard, etc.). In some embodiments, one or more of the illustrative components may be incorporated in, or otherwise form a portion of, another component. The compute engine 210 may be embodied as any type of device or collection of devices capable of performing various compute functions described below. In some embodiments, the compute engine 210 may be embodied as a single device such as an integrated circuit, an embedded system, a field-programmable gate array (FPGA), a system-on-a-chip (SOC), or other integrated system or device. Additionally, in the illustrative embodiment, the compute engine 210 includes or is embodied as a processor 212 and a memory 214. The processor 212 may be embodied as any type of processor capable of performing the functions described herein. For example, the processor 212 may be embodied as a single or multi-core processor(s), a microcontroller, or other processor or processing/controlling circuit. In some embodiments, the processor 212 may be embodied as, include, or be coupled to an FPGA, an application specific integrated circuit (ASIC), reconfigurable hardware or hardware circuitry, or other specialized hardware to facilitate performance of the functions described herein.|[0045] In embodiments, the processor 212 is capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, a set of instructions which when executed by the processor 212 cause the modeling compute device 120 to perform one or more operations described herein. In embodiments, the processor 212 is further capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, one or more signals from external sources, e.g., from the peripheral devices 226 or via the communication circuitry 218 from an external compute device, external source, or external network. As one will appreciate, a signal may contain encoded instructions and/or information. In embodiments, once received, such a signal may first be stored, e.g., in the memory 214 or in the data storage device(s) 222, thereby allowing for a time delay in the receipt by the processor 212 before the processor 212 operates on a received signal. Likewise, the processor 212 may generate one or more output signals, which may be transmitted to an external device, e.g., an external memory or an external compute engine via the communication circuitry 218 or, e.g., to one or more display devices 224. In some embodiments, a signal may be subjected to a time shift in order to delay the signal. For example, a signal may be stored on one or more storage devices 222 to allow for a time shift prior to transmitting the signal to an external device. One will appreciate that the form of a particular signal will be determined by the particular encoding a signal is subject to at any point in its transmission (e.g., a signal stored will have a different encoding than a signal in transit, or, e.g., an analog signal will differ in form from a digital version of the signal prior to an analog-to-digital (A/D) conversion).|[0046] The main memory 214 may be embodied as any type of volatile (e.g., dynamic random access memory (DRAM), etc.) or non-volatile memory or data storage capable of performing the functions described herein. Volatile memory may be a storage medium that requires power to maintain the state of data stored by the medium. In some embodiments, all or a portion of the main memory 214 may be integrated into the processor 212. In operation, the main memory 214 may store various software and data used during operation such as models, databases, simulation results, applications, libraries, and drivers.|[0047] The compute engine 210 is communicatively coupled to other components of the modeling compute device 120 via the I/O subsystem 216, which may be embodied as circuitry and/or components to facilitate input/output operations with the compute engine 210 (e.g., with the processor 212 and the main memory 214) and other components of the modeling compute device 120. For example, the I/O subsystem 216 may be embodied as, or otherwise include, memory controller hubs, input/output control hubs, integrated sensor hubs, firmware devices, communication links (e.g., point-to-point links, bus links, wires, cables, light guides, printed circuit board traces, etc.), and/or other components and subsystems to facilitate the input/output operations. In some embodiments, the I/O subsystem 216 may form a portion of a system-on-a-chip (SoC) and be incorporated, along with one or more of the processor 212, the main memory 214, and other components of the modeling compute device 120, into the compute engine 210.|[0048] The communication circuitry 218 may be embodied as any communication circuit, device, or collection thereof, capable of enabling communications over a network between the modeling compute device 120 and another device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). The communication circuitry 218 may be configured to use any one or more communication technology (e.g., wired or wireless communications) and associated protocols (e.g., Ethernet, Wi-Fi®, WiMAX, Bluetooth®, etc.) to effect such communication.|[0049] The illustrative communication circuitry 218 includes a network interface controller (NIC) 220. The NIC 220 may be embodied as one or more add-in-boards, daughter cards, network interface cards, controller chips, chipsets, or other devices that may be used by the modeling compute device 120 to connect with another compute device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). In some embodiments, the NIC 220 may be embodied as part of a system-on-a-chip (SoC) that includes one or more processors, or included on a multichip package that also contains one or more processors. In some embodiments, the NIC 220 may include a local processor (not shown) and/or a local memory (not shown) that are both local to the NIC 220. Additionally or alternatively, in such embodiments, the local memory of the NIC 220 may be integrated into one or more components of the modeling compute device 120 at the board level, socket level, chip level, and/or other levels.|[0050] Each data storage device 222, may be embodied as any type of device configured for short-term or long-term storage of data such as, for example, memory devices and circuits, memory cards, hard disk drives, solid-state drives, or other data storage device. Each data storage device 222 may include a system partition that stores data and firmware code for the data storage device 222 and one or more operating system partitions that store data files and executables for operating systems.|[0051] Each display device 224 may be embodied as any device or circuitry (e.g., a liquid crystal display (LCD), a light emitting diode (LED) display, a cathode ray tube (CRT) display, etc.) configured to display visual information (e.g., text, graphics, etc.) to a user. In some embodiments, a display device 224 may be embodied as a touch screen (e.g., a screen incorporating resistive touchscreen sensors, capacitive touchscreen sensors, surface acoustic wave (SAW) touchscreen sensors, infrared touchscreen sensors, optical imaging touchscreen sensors, acoustic touchscreen sensors, and/or other type of touchscreen sensors) to detect selections of on-screen user interface elements or gestures from a user.|[0052] In the illustrative embodiment, the components of the modeling compute device 120 are housed in a single unit. However, in other embodiments, the components may be in separate housings, in separate racks of a data center, and/or spread across multiple data centers or other facilities. The compute devices 140, 142, 144, 150, 152, 154 may have components similar to those described in FIG. 2 with reference to the modeling compute device 120. The description of those components of the modeling compute device 120 is equally applicable to the description of components of the compute devices 140, 142, 144, 150, 152, 154. Further, it should be appreciated that any of the devices 120, 140, 142, 144, 150, 152, 154 may include other components, sub-components, and devices commonly found in a computing device, which are not discussed above in reference to the modeling compute device 120 and not discussed herein for clarity of the description.|[0053] In the illustrative embodiment, the compute devices 120, 140, 142, 144, 150, 152, 154 are in communication via a network 160, which may be embodied as any type of wired or wireless communication network, including global networks (e.g., the internet), wide area networks (WANs), local area networks (LANs), digital subscriber line (DSL) networks, cable networks (e.g., coaxial networks, fiber networks, etc.), cellular networks (e.g., Global System for Mobile Communications (GSM), Long Term Evolution (LTE), Worldwide Interoperability for Microwave Access (WiMAX), 3G, 4G, 5G, etc.), a radio area network (RAN), or any combination thereof.|[0054] Referring now to FIG. 3, the system 100 (e.g., a modeling compute device 120 of the gateway 110) may perform a method 300 for modeling carbon dioxide removal through enhanced rock weathering. The method 300, in the illustrative embodiment, begins with block 302 in which the modeling compute device 120 obtains parameter data indicative of parameters for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering (e.g., the application of basalt dust to soil to increase the amount of carbon dioxide captured through the interaction of water (e.g., rain), carbon dioxide, and rock (e.g., the basalt dust)). In doing so, and as indicated in block 304, the modeling compute device 120 obtains data indicative of properties of soil in a location where the carbon dioxide is to be captured (e.g., removed from the atmosphere through enhanced rock weathering). In the illustrative embodiment, the modeling compute device 120 may obtain data indicative of minerals in the soil (e.g., a numeric value, such as a number indicative of a percentage of the soil comprising minerals), as indicated in block 306. As indicated in block 308, the modeling compute device 120 may obtain data indicative of carbon in the soil (e.g., a numeric value indicative of a percentage of the soil comprising carbon).|[0055] The modeling compute device 120 may additionally obtain data indicative of effective porosity of the soil where the carbon is to be captured, as indicated in block 310. The effective porosity may be expressed, in at least some embodiments, as a numeric value (e.g., a percentage). As indicated in block 312, the modeling compute device 120 may obtain parameter data indicative of total specific surface area. In at least some embodiments, the total specific surface area may be expressed as square meters per gram. The modeling compute device 120 may obtain data indicative of the height of a top soil layer, as indicated in block 314. The height, in the illustrative embodiment, is expressed in meters. Further, the modeling compute device 120 may obtain data indicative of an amount of basalt added to the soil (e.g., tons per hectare), as indicated in block 316. Further, the modeling compute device 120 may obtain data indicative of basalt density, such as in grams per cubic centimeter, as indicated in block 318. Additionally, the modeling compute device 120 may obtain data indicative of bulk soil density, as indicated in block 320. The bulk soil density, in at least some embodiments, may be expressed as grams per cubic centimeter. The modeling compute device 120 may also obtain data indicative of basalt mineral composition, as indicated in block 322. The mineral composition of the basalt may be structured as one or more pairs of values, with each pair including an identifier (e.g., name, abbreviation, etc.) of a mineral and a corresponding percentage (e.g., indicative of a percentage of the basalt feed stock that the mineral constitutes).|[0056] Still referring to FIG. 3, the modeling compute device 120 may obtain the parameter data as a function of (e.g., based on) an identification of the location where the carbon dioxide is to be captured in the soil, as indicated in block 324. In doing so, the modeling compute device 120 may read parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of properties of soil associated with location identifiers (e.g., plot numbers, geographic coordinates, zip codes, etc.), as indicated in block 326. In some embodiments, the modeling compute device 120 may obtain parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of mineral compositions from each of multiple basalt feed stocks, as indicated in block 328. Additionally or alternatively, the modeling compute device 120 may obtain parameter data through user input into corresponding fields (e.g., text boxes, check boxes, etc.) of a user interface (e.g., a graphical user interface presented by a target compute device 150, 152, 154 based on code (e.g., hypertext markup language (HTML) and/or JavaScript) and images (e.g., portable network graphics (PNG) files, Joint Photographic Experts Group (JPEG) files, or the like) transmitted from the modeling compute device 120 to the target compute device(s) 150, 152, 154 via the network 160, as indicated in block 330. An embodiment of a user interface 800 with which the modeling compute device 120 may obtain parameter data is shown in FIG. 8. The user interface 800 includes a first screen 810 that comprises parameter data about soil properties and a second screen 820 that includes parameter data about basalt mineral makeup. The user interface 800 provides one embodiment that users can use to input parameters related to soil properties and basalt mineral composition, run the models, and calculate how much CO2 can be sequestered.|[0057] Referring now to FIG. 4, the method 300 continues in block 332 in which the modeling compute device 120 may calculate, as a function of the obtained parameter data, additional parameter data for use by one or more models (e.g., the models 130). In doing so, the modeling compute device 120 may calculate air and blind pores (e.g., a numeric value), as indicated in block 334. The modeling compute device 120 may additionally calculate a volume of soil per hectare, as indicated in block 336. Further, the modeling compute device 120 may calculate a number of volume (e.g., liters) of pore water per unit of area (e.g., hectare), as indicated in block 338. Additionally, the modeling compute device 120 may calculate a mass of basalt per unit of volume of the soil, as indicated in block 340. In addition, the modeling compute device 120 may calculate a concentration of basalt in the soil, as indicated in block 342. Further, the modeling compute device 120 may calculate a total weight percentage, as indicated in block 344. The modeling compute device 120 may also calculate a rock specific surface area, as indicated in block 346. In addition, the modeling compute device 120 may calculate a total surface area, in block 348. In performing the calculations, the modeling compute device 120 may utilize a database (e.g., a database 132) of specific surface areas for each of a set of minerals (e.g., minerals in the soil, in the basalt, etc.), as indicated in block 350. An embodiment of a user interface 900 in which the modeling compute device 120 may display additional parameters calculated as discussed above is shown in FIG. 9. In some embodiments, the user interface 800 includes a third screen 830 that may display additional parameters calculated as discussed above.|[0058] After obtaining the parameter data, the method 300, in the illustrative embodiment, advances to block 352, in which the modeling compute device 120 produces, using one or models from a library of models (e.g., the models 130), one or more predictions indicative of an amount of carbon dioxide that will be removed from the atmosphere (e.g., captured through enhanced rock weathering). In doing so, the modeling compute device 120 may select one or more models 130 as a function of the obtained parameter data, as indicated in block 354. That is, the modeling compute device 120 may select one or more models 130 from the library of models as a function of a determined similarity (e.g., a similarity score, such as a calculated distance (e.g., a Euclidean distance, a cosine similarity, a result of a clustering analysis, etc.)) of the parameter data (e.g., obtained in block 302) to reference parameters for which one or more corresponding models 130 have been identified (e.g., in a data set in the memory 214 or storage 222, in a database 132, etc.) as having a high accuracy of predictions (e.g., the results 134 produced by those models have been shown to predict within a predefined threshold of accuracy (e.g., a defined percentage), actual results that were later measured in field tests). That is, if a particular model 130 is identified as more accurately predicting the amount of carbon dioxide that will be removed from the atmosphere than other models, when the parameters are similar to those obtained in block 302, the modeling compute device 120 may select that model for use.|[0059] In some embodiments, as indicated in block 358, the modeling compute device 120 may select one or more models 130 as a function of a distance of the location where the carbon dioxide is to be captured to each of a set of reference locations associated with the models 130. That is, a data set (e.g., in the memory 214, the data storage 222, or a database 132) may identify a location (e.g., a zip code, a set of geographic coordinates, or other identifier of a location) with each model 130 in the library (e.g., because the corresponding model 130 has been shown to produce predictions with high accuracy for the associated location) and the modeling compute device 120 may select a set (e.g., one or more) of the models 130 that are closest to the location where the carbon dioxide is to be captured.|[0060] Referring now to FIG. 5, in block 360, the modeling compute device 120 may reformat the parameter data for use by the models 130 (e.g., by converting the data into a file format that the models 130 are configured to parse (e.g., using a scripting language such as Python)). As indicated in block 362, the modeling compute device 120 may select one or more machine learning models (e.g., models, such as neural networks, decision trees, or others that may iteratively improve in prediction accuracy based on feedback). In some embodiments, the modeling compute device 120 may select an ensemble (e.g., a combination of models, in which outputs of the individual models may be weighted relative to each other), as indicated in block 364. The models 130 may include one or more models implemented by PHREEQC (e.g., PHREEQC 3), from the U.S. Geological Survey, GEM (e.g., reservoir modeling), TOUGHREACT from Lawrence Berkeley National Laboratory, and/or other models (e.g., provided by entities associated with one or more of the source compute devices 140, 142, 144). The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period, as indicated in block 366. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured each year of a defined number of years at the specified location, as indicated in block 368.|[0061] The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per unit of area, as indicated in block 370. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per hectare, as indicated in block 372. In the illustrative embodiment, and unlike conventional systems, the modeling compute device 120 utilizes models that simulate co-precipitation of iron with toxic metals, as indicated in block 374. Additionally, and unlike conventional systems, the modeling compute device 120, in the illustrative embodiment, utilizes models that simulate basalt weathering as irreversible reactions with unidirectional rates, as indicated in block 376. Further, and unlike conventional systems, the modeling compute device 120 in the illustrative embodiment utilizes models in which near-equilibrium (e.g., within a defined percentage of an equilibrium state) rates are one to two orders of magnitude slower than far-from-equilibrium (e.g., not within the defined percentage of the equilibrium state) rates, as indicated in block 378. Further, and as indicated in block 380, the modeling compute device 120, in the illustrative embodiment, produces one or more predictions indicative of toxic metal concentrations in water associated with the location where the carbon dioxide is to be captured. In doing so, the modeling compute device 120 may produce one or more predictions indicative of concentrations of Nickel, Chromium, and/or Cadmium in the water, as indicated in block 382.|[0062] Referring now to FIG. 6, the modeling compute device 120 may produce the one or more predications as a function of depth (e.g., depth of the water), as indicated in block 384. As indicated in block 386, the modeling compute device 120 may produce the one or more predictions regarding toxic metals in the water as a function of time (e.g., amount of toxic metals in the water per year). In some embodiments, the modeling compute device 120 may produce the predictions of toxic metals in the water relative to one or more regulations associated with the location where the carbon dioxide is to be captured, as indicated in block 388. That is, the modeling compute device 120 may obtain data (e.g., from a database 132, from a source compute device 140, 142, 144) indicative of applicable regulations and indicate whether the predicted amount of toxic metals satisfies (e.g., does not violate the regulation(s), is close to (e.g., within a defined percentage of), etc.) a limit specified by the regulations. The modeling compute device 120 may produce the prediction(s) relative to drinking water regulations and/or irrigation water regulations, as indicated in blocks 390, 392. The modeling compute device 120 may produce one or more predictions indicative of toxic metal concentrations in the soil associated with the location where the carbon dioxide is to be captured, as indicated in block 394. In doing so, the modeling compute device 120 may produce prediction(s) indicative of concentrations of Nickel, Chromium, and/or Cadmium in the soil, as indicated in block 396. The modeling compute device 120 may produce the prediction(s) as a function of depth (e.g., in the soil) and/or as a function of time, as indicated in blocks 398, 400. Similar to block 388, the modeling compute device 120 may produce the prediction(s) of toxic metals in the soil relative to one or more regulations associated with the location, as indicated in block 402.|[0063] Referring now to FIG. 7, the modeling compute device 120 may produce data indicative of probabilities (e.g., confidence) associated with the one or more predictions, as indicated in block 404. For example, the modeling compute device 120 may produce a predictions as confidence intervals, with one prediction associated with a particular level of confidence (e.g., a percentage of likelihood), and one or more other predictions associated with other levels of confidence. As indicated in block 406, the modeling compute device 120 may determine an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. For example, the modeling compute device 120 may obtain data (e.g., from a source compute device 140, 142, 144, a database 132, etc.) indicative of a conversion rate between tons of carbon captured and a number of corresponding carbon credits and multiply the predicted amount of carbon dioxide by the conversion rate to determine the amount of carbon credits. In some embodiments, the modeling compute device 120 may adjust the number of carbon credits based on a probability or confidence level associated with the predicted amount of carbon dioxide to be removed from block 404 (e.g., by multiplying the amount of carbon dioxide by a percentage associated with the probability or confidence level). As indicated in block 408, the modeling compute device 120 may determine soil parameters that will increase capture of carbon dioxide at the location. For example, and as indicated in block 410, the modeling compute device 120 may determine, from a set of multiple basalt feed stocks, each having different mineral compositions and/or other properties, a basalt feed stock predicted to capture the most carbon dioxide in the location while maintaining compliance with regulations (e.g., toxic metals in the soil, toxic metals in the water). The modeling compute device 120 may do so by simulating carbon dioxide capture with each of the basalt feed stocks using the models 130 and identifying the basalt feed stock that satisfies the above conditions to the greatest degree.|[0064] Continuing the method 300, the modeling compute device 120 may present a visual representation of the one or more prediction(s) in a user interface, as indicated in block 412. In the illustrative embodiment, the modeling compute device 120 produces visual presentation(s) of the prediction(s) in a web based interface (e.g., based on a HTML, JavaScript, and image data sent from the modeling compute device 120 to one or more rending engines (e.g., web browser(s)) executed by corresponding target compute devices 150, 152, 154). As indicated in block 416, in producing one or more visual representations of the prediction(s), the modeling compute device 120 may present visual representations that include interactive graphs (e.g., in which time periods, depths, or other parameters may be selected and a corresponding graph is presented). Example embodiments of visual representations 1000, 1100, 1200, 1300, 1400 of the predictions that may be presented by the modeling compute device 120 and displayed by one or more of the corresponding target compute devices 150, 152, 154 are shown in FIGS. 10-14.|[0065] While certain illustrative embodiments have been described in detail in the drawings and the foregoing description, such an illustration and description is to be considered as exemplary and not restrictive in character, it being understood that only illustrative embodiments have been shown and described and that all changes and modifications that come within the spirit of the disclosure are desired to be protected. There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein. It will be noted that alternative embodiments of the apparatus, systems, and methods of the present disclosure may not include all of the features described, yet still benefit from at least some of the advantages of such features. Those of ordinary skill in the art may readily devise their own implementations of the apparatus, systems, and methods that incorporate one or more of the features of the present disclosure. Family Number|(117356463)|117356463|Abstract|(US20260017435 A1)|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed.|CPC codes|(US20260017435 A1)|B01D-053/62|B01D-053/82|B01D-2257/504|IPC codes|(US20260017435 A1)|B01D-053/62|B01D-053/82|Title|(US20260017435 A1)|Technologies for modeling carbon dioxide removal| Computer technology|Environmental technology B01D-053/62|B01D-053/82|B01D-2257/504|G06F-030/27 B01D-053/62|B01D-053/82|B01D-2257/504|G06F-030/27 B01D-053/62|B01D-053/82|G06F-030/27 B01D-053/62|B01D-053/82|G06F-030/27 PENDING (US20260017435)|PENDING ALIVE (US20260017435)|ALIVE (US20260017435)|LEGAL DETAILS FOR US20260017435|Actual or expected expiration date=2045-07-09|Legal state=ALIVE|Status=PENDING|Event publication date=2025-07-09|Event code=US/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=US US19264502|Application date=2025-07-09|Standardized application number=2025US-19264502|Event publication date=2025-07-09|Event code=US/EXMR|Event group=Administrative notifications|USPTO Examiner Name|PRIMARY EXAMINER:CENTRAL, DOCKET|Event publication date=2025-07-09|Event code=US/ART|Event group=Administrative notifications|USPTO Art Group|ART=OPAP|Event publication date=2025-07-09|Event code=US/DK|Event group=Examination events|Attorney Docket Number|Docket Nbr: 29920-426689|Event publication date=2025-07-09|Event code=US/CUST|Event group=Examination events|Attorney/Agent Customer Number|Customer Nbr: 138060|Event publication date=2025-07-09|Event code=US/SMALL|Event group=Administrative notifications|Appl Has Filed a Verified Statement of Micro to Small Entity Status|Business Entity Status: Small|Event publication date=2025-07-09|Event code=US/AIA|Event group=Administrative notifications|First Inventor File Indicated:|AIA=Yes|Event publication date=2025-07-09|Event code=US/ENT|Event group=Administrative notifications|Entity Status Set to Undiscounted|Event publication date=2025-07-25|Event code=US/SMALL|Event group=Administrative notifications|Appl Has Filed a Verified Statement of Micro to Small Entity Status|Event publication date=2025-07-29|Event code=US/APPFILEREC|Event group=Administrative notifications OAO|Filing Receipt|Event publication date=2025-09-29|Event code=US/PTARDY|Event indicator=Pos|Event group=Examination events|Patent Term Adjustment - Ready for Examination|Event publication date=2025-10-02|Event code=US/RECEIPTUP|Event group=Administrative notifications OAO|Filing Receipt - Updated|Event publication date=2025-10-22|Event code=US/DKNC|Event indicator=Pos|Event group=Examination events|Docketed New Case - Ready for Examination|Event publication date=2025-10-22|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2026-01-15|Event code=US/A1|Event group=Examination events|Application published|Publication country=US|Publication number=US20260017435|Publication stage code=A1|Publication date=2026-01-15|Standardized publication number=US20260017435|Event publication date=2026-01-16|Event code=US/PGPUBN|Event indicator=Pos|Event group=Examination events OAO|PG-Pub Issue Notification (US20260017435)|US https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcP7LGmymc8G11q5LJ03xVJIJjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023247689&ekey=1952&xpn=US20260017435&kind=A1 https://data.uspto.gov/patent-file-wrapper/search/details/19264502/application-data https://permalink.orbit.com/RenderStaticFirstPage?XPN=rCUZBbi%252Bv%252B%252FyiDX9GDUoPcRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT US (US20260017435)|US (US20260017435)|NAME=THE TRUSTEES OF INDIANA UNIVERSITY , CITY=Bloomington , STATE=IN , COUNTRY=US (US20260017435)|US (US20260017435)|NAME=Zhu Chen, CITY=Bloomington, STATE=IN , COUNTRY=US 0 1 Titre: (US20260017435)|Technologies for modeling carbon dioxide removal Résumé: (US20260017435)|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed. 38 Abstract gpt-4o-mini yes The article discusses enhanced rock weathering as a method for carbon dioxide removal, which aligns with the topic of accelerated weathering of rocks for CO₂ capture.
40 CN202510409398 CN202510409398 CN120242698 115152801 CN120242698 A 2025-07-04 [CN120242698] 2025-04-02 2025-04-02 2025-07-04 (CN120242698)|2045-04-02 (CN120242698)|Method for realizing carbon sequestration by using alkalinity source (CN120242698)|The invention provides a method for realizing carbon sequestration by using an alkalinity source, which comprises the following steps: (1) grinding, crushing and screening the alkalinity source to obtain alkalinity source powder; wherein the alkalinity source is prepared from peridotite, basalt, wollastonite and anorthite; (2) carrying out acid leaching on the alkalinity source powder to obtain an ore leaching suspension; reacting the mineral leaching suspension liquid with a pretreatment agent under the conditions that the temperature is 150 DEG C, the pressure is 5MPa and the liquid-solid ratio is 20: 1 to obtain a pretreated alkalinity source; (3) mixing the pretreated alkalinity source with water, and then introducing carbon dioxide gas to carry out carbonation reaction; after the reaction is finished, a gas channel is closed, and carbonate rock minerals are obtained after cooling and solid-liquid separation, so that carbon sequestration is realized, and permanent, stable and large-scale sequestration of carbon dioxide can be realized. JIANGXI UNIVERSITY OF SCIENCE & TECHONOLOGY (CN120242698)|JIANGXI UNIVERSITY OF SCIENCE & TECHONOLOGY ([CN]) HE YANXIN|WANG LISHUANG|WEI MINGCONG|DENG ZHAOSHAN (CN120242698)|HE YANXIN|WANG LISHUANG|WEI MINGCONG|DENG ZHAOSHAN (CN120242698)|LIU JINRONG;CHENGDU RUI DAO ZHICHENG PATENT AGENCY CO., LTD.|Reg. Nb: 51217 (CN120242698)|Based on this, when carbon dioxide is sequestered, if dry carbonation is adopted, that is, carbonate is obtained directly by using a gas-solid one-step reaction mode, but the method needs to be carried out at high temperature and high pressure to isolate carbon dioxide from the atmosphere, however, one major disadvantage of the method is that the reaction kinetics of calcium silicate and magnesium silicate are often too slow, and the acceleration of the reaction kinetics by increasing the temperature is often thermodynamically limited.| (CN120242698)|1.A method for achieving carbon sequestration using an alkalinity source, comprising the steps of: (1) Grinding and crushing the alkalinity source and screening to obtain alkalinity source powder with the particle size of 30-50 mu m; (2) Acid leaching is carried out on the alkalinity source powder to obtain an ore leaching suspension, and then the ore leaching suspension reacts with a pretreatment agent under the conditions of 150 ℃ and 5MPa and a liquid-solid ratio of 20:1 to obtain a pretreatment alkalinity source; (3) And after the reaction is finished, closing a gas channel, cooling and carrying out solid-liquid separation to obtain carbonate minerals, thereby realizing the carbon sealing.| (CN120242698)|The invention provides a method for realizing carbon sequestration by utilizing an alkalinity source, which comprises the following steps of (1) grinding and crushing the alkalinity source and screening to obtain alkalinity source powder, wherein the alkalinity source comprises olivine, basalt, wollastonite and anorthite, (2) carrying out acid leaching on the alkalinity source powder to obtain a mineral leaching suspension, then reacting the mineral leaching suspension with a pretreatment agent under the conditions of 150 ℃ and 5MPa and a liquid-solid ratio of 20:1 to obtain a pretreated alkalinity source, (3) mixing the pretreated alkalinity source with water, then introducing carbon dioxide gas for carbonation reaction, closing a gas channel after the reaction is finished, and obtaining carbonate mineral after cooling and solid-liquid separation, thereby realizing the sequestration of carbon and realizing the permanent, stable and large-scale sequestration of carbon dioxide.|The invention relates to the technical field of carbon dioxide sealing and storage, in particular to a method for realizing carbon sealing and storage by utilizing an alkalinity source.| (CN120242698)|ALKALINITY SOURCE(100,58)|CARBON SEQUESTRATION(100,24)|MINERAL LEACHING SUSPENSION(99,18)|PRETREATMENT(51,36)|WOLLASTONITE MINERAL LEACHING SUSPENSION(50,2)|BASALT MINERAL LEACHING SUSPENSION(49,5)|PRETREATED ALKALINITY SOURCE(48,10)|ANORTHITE MINERAL LEACHING SUSPENSION(47,5)|DRY CARBONATION(41,1)|CARBONATION REACTION(39,13)|ANORTHITE PRETREATMENT(39,2)|WOLLASTONITE PRETREATMENT(39,2)|REALIZING CARBON SEALING(39,1)|BASALT PRETREATMENT(38,2)|OLIVINE PRETREATMENT(38,2)|PRETREATMENT ALKALINITY SOURCE(33,5)|CARBON SEALING(33,1)|CARBONATE MINERAL(32,14)|ALKALINITY SOURCE POWDER(30,8)|OLIVINE(28,12)|ANORTHITE(27,6)|WOLLASTONITE(26,9)|GRINDING(26,6)|CALCIUM SILICATE REACTION KINETICS(26,1)|ACCELERATION(25,1)|BASALT(24,6)|GAS CHANNEL(24,6)|ORE(23,10)|REACTION KINETICS(23,2)|CARBON DIOXIDE SEALING(21,1)|MAGNESIUM SILICATE(21,1)|CARBON DIOXIDE(20,44)|ACID LEACHING(20,15)|CALCIUM SILICATE(20,1)|ACIDIC LIQUOR(19,2)|CARBON DIOXIDE DISCHARGE TOWER(17,2)|REACTION MODE(17,1)|CARBON DIOXIDE GAS(16,8)|SOLID LIQUID SEPARATION(16,3)|PRETREAT OLIVINE(15,3)|PRETREAT WOLLASTONITE(15,3)|MAGNESIUM ION(14,10)|NACL(13,12)|STIRRING SPEED(13,9)|LARGE SCALE SEQUESTRATION(13,2)|LIQUID SOLID RATIO(11,8)|TOO SLOW(10,1)|SUSPENSION LIQUID MINERAL LEACHING(9,3)|PARTICLE SIZE(8,6)|BICARBONATE ION(8,4)|REACTION KETTLE(8,4)|PICKLING TIME(8,1)|SAFE SEQUESTRATION(8,1)|WOLLASTONITE DISSOLUTION(8,1)|CARBONATION CONVERSION RATE(7,5)|ACID LEACHING PRETREATMENT(7,3)|LEACHING SUSPENSION LIQUID(7,3)|GEOLOGICAL SEALING(7,2)|MARINE SEALING(7,2)|STABLE CARBONATE MINERAL(7,2)|ACETIC ACID(6,5)|SULFURIC ACID(6,5)|INORGANIC SEALING(6,2)|ADVOCATING GREEN(6,1)|BASALT ROCK(6,1)|DECOMPOSED CARBONATE ION(6,1)|MANUFACTURER ATTENTION(6,1)|METALLURGICAL PLANT(6,1)|OLIVINE ROCK(6,1)|REACTION CONDITION(6,1)|RELIABLE SEQUESTRATION(6,1)|STABLE CARBONATE ROCK MINERAL(6,1)|MASS RATIO(5,10)|NAHCO(5,4)|POWER PLANT TOWER(5,3)|CALCIUM MIGRATION(5,1)|CARBON DIOXIDE MINERAL SEQUESTRATION(5,1)|R MIN(5,1)|WET CARBONATION MODE(5,1)|ALKALINITY SOURCE DIFFERENCE(4,2)|ALKALINITY SOURCE DISPERSION(4,1)|ALKALINITY SOURCE DISSOLUTION REACTION(4,1)|BICARBONATE RADICAL ION(4,1)|CALCIUM CARBONATE SOLUBILITY(4,1)|CARBON DIOXIDE EMISSION TOWER(4,1)|CARBON DIOXIDE SEQUESTRATION(4,1)|CARBON INVENTORY(4,1)|CARBONATE RADICAL REDUCTION(4,1)|FEASIBILITY(4,1)|HYDROCHLORIC ACID TITRATION(4,1)|LEAKAGE RISK(4,1)|MINERAL SEALING(4,1)|OCCUPATION RATIO(4,1)|PERMANENT SEALING(4,1)|SALT ION(4,1)|STOICHIOMETRIC RELATION(4,1)| (CN120242698)|1. A method for achieving carbon sequestration using an alkalinity source, comprising the steps of:| (1) Grinding and crushing the alkalinity source and screening to obtain alkalinity source powder with the particle size of 30-50 mu m; | (2) Acid leaching is carried out on the alkalinity source powder to obtain an ore leaching suspension, and then the ore leaching suspension reacts with a pretreatment agent under the conditions of 150 ℃ and 5MPa and a liquid-solid ratio of 20:1 to obtain a pretreatment alkalinity source; | (3) And after the reaction is finished, closing a gas channel, cooling and carrying out solid-liquid separation to obtain carbonate minerals, thereby realizing the carbon sealing. |2. The method for carbon sequestration using an alkalinity source according to claim 1, wherein in step (1), the alkalinity source is ground and crushed and sieved to a particle size of 30-50 μm.|3. The method for carbon sequestration using an alkalinity source according to claim 1, wherein in step (1), the alkalinity source comprises olivine, basalt, wollastonite, anorthite.|4. The method for carbon sequestration using an alkalinity source according to claim 1, wherein in step (2), when the alkalinity source powder is subjected to acid leaching, the acid liquor used is different according to the alkalinity source, concretely comprising the steps of pretreatment of olivine with sulfuric acid, pretreatment of basalt with hydrochloric acid, pretreatment of wollastonite with hydrochloric acid, and pretreatment of anorthite with acetic acid.|5. The method for carbon sequestration using an alkalinity source according to claim 4, wherein in step (2), the pretreatment agents used are different depending on the alkalinity source, and specifically, the pretreatment agents added to the olivine and anorthite mineral leaching suspensions are 0.50mol/L NaHCO 3 and 1.00mol/L NaCl, the pretreatment agents added to the basalt mineral leaching suspensions are 0.50mol/L NaHCO 3, and the pretreatment agents added to the wollastonite mineral leaching suspensions are 0.50mol/L NaHCO 3 and 0.25mol/L NaCl.|6. The method for carbon sequestration using an alkalinity source according to claim 1, wherein in step (2), the liquid-solid ratio at the time of pickling is 10-20:1ml/g.|7. The method for carbon sequestration using an alkalinity source according to claim 1, wherein in step (2), the mass ratio of the mineral leaching suspension to the pretreatment agent is 10-20:1.|8. The method for carbon sequestration using an alkalinity source according to claim 1, wherein the reaction conditions for the carbonation reaction in step (3) are 100 to 200 ℃ and 5 to 10MPa.|9. The method for carbon sequestration using an alkalinity source according to claim 1, wherein in step (3), the reaction is carried out for 0.5 to 1.5 hours under stirring speed of 200 to 300 r/min.|10. The method for carbon sequestration using an alkalinity source according to claim 1, wherein in step (3), the carbon dioxide gas is derived from a carbon dioxide discharge tower. (CN120242698)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of carbon dioxide sealing and storage, in particular to a method for realizing carbon sealing and storage by utilizing an alkalinity source.|BACKGROUND ART|[0002] As the greenhouse gas content in the atmosphere gradually increases, the global climate changes significantly and the atmospheric concentration of carbon dioxide increases significantly.|[0003] At present, the internationally common carbon dioxide control technology mainly comprises three steps of (1) reducing the use of non-renewable energy sources such as fossil fuel (coal, petroleum and natural gas), developing and utilizing renewable energy sources such as geothermal energy, wind energy and biomass energy, reducing the occupation ratio of primary energy consumption by changing an energy structure, (2) improving the energy conversion efficiency, advocating green and energy-saving life, and (3) adopting a carbon dioxide capturing and sealing technology (CCS). Among them, CCS technology is considered as one of the most promising technologies for solving the greenhouse effect, and has a certain feasibility in the treatment of large-scale carbon dioxide sources.|[0004] The carbon dioxide sealing mode mainly comprises geological sealing, mineral sealing and marine sealing, wherein the geological sealing is to pour carbon dioxide into a proper stratum under pressure, the carbon dioxide is stored in the pore space of the stratum, the mineral sealing is to enable the carbon dioxide to chemically react with metal oxide to form carbonate and other byproducts in solid forms, and the marine sealing is to pour liquid carbon dioxide into a deep sea water area to form a stable lake-shaped structure under high-pressure conditions.|[0005] The mineral sealing and storage method utilizes the chemical reaction of carbon dioxide and certain minerals (such as olivine) to generate stable carbonate minerals, and the sealing and storage method is stable and has no leakage risk. And most of carbon on the earth exists in the form of carbonate minerals, and carbon sequestration in the crystal structure of the minerals is a long-lasting and reliable method, so carbon dioxide mineral sequestration is acknowledged as the safest and reliable sequestration method.|[0006] Based on this, when carbon dioxide is sequestered, if dry carbonation is adopted, that is, carbonate is obtained directly by using a gas-solid one-step reaction mode, but the method needs to be carried out at high temperature and high pressure to isolate carbon dioxide from the atmosphere, however, one major disadvantage of the method is that the reaction kinetics of calcium silicate and magnesium silicate are often too slow, and the acceleration of the reaction kinetics by increasing the temperature is often thermodynamically limited. It is therefore important to find a suitable and stable wet carbonation for carbon dioxide sequestration.|DISCLOSURE|Disclosure of Invention|[0007] Based on the above problems, it is an object of the present invention to provide a method for carbon sequestration using an alkalinity source which allows permanent, stable and large scale sequestration of carbon dioxide.|[0008] The inventor seeks to sequester carbon dioxide in a wet carbonation manner, however, in research and practice the inventor has found that calcium and magnesium ions migrate to the surface of the mineral during the reaction to form carbonate minerals, which encapsulate the mineral and hinder the carbonation reaction and thus affect the sequestering effect. Therefore, the method comprises the steps of firstly carrying out acid leaching pretreatment on an alkalinity source before reaction, firstly dissolving out partial calcium and magnesium ions preferentially, then carbonating the pretreated alkalinity source with carbon dioxide, dissolving the carbon dioxide in a liquid phase to generate carbonic acid, decomposing the carbonic acid into carbonate ions or bicarbonate ions, dissolving out metal ions by the alkalinity source under the proton exchange effect, and carrying out chemical precipitation with the carbonic acid decomposed carbonate ions or bicarbonate ions to form stable carbonate rock mineral, thereby realizing the carbon sequestration.|[0009] The implementation mode of the invention is realized by the following technical scheme:|[0010] a method for carbon sequestration using an alkalinity source comprising the steps of: |[0011] (1) Grinding and crushing an alkalinity source and screening the alkalinity source to the particle size of 30-50 mu m to obtain alkalinity source powder, wherein the alkalinity source comprises olivine, basalt, wollastonite, anorthite and the like; |[0012] (2) Acid leaching is carried out on the alkalinity source powder, the liquid-solid ratio during acid leaching is 10-20:1mL/g, thus obtaining an ore leaching suspension, and then the ore leaching suspension and a pretreatment agent are mixed according to the mass ratio of 10-20:1 for reaction, thus obtaining a pretreatment alkalinity source; |[0013] (3) Mixing a pretreated alkalinity source and water according to a mass ratio of 1:10-20, adding the mixture into a reaction kettle, stirring the mixture for 5-20min at a stirring speed of 200-300r/min, then introducing carbon dioxide gas, wherein the carbon dioxide gas can be sourced from a carbon dioxide discharge tower or other carbon dioxide discharge towers of a thermal power plant, and carrying out carbonation reaction for 0.5-1.5h at a stirring speed of 200-300r/min under the conditions of 100-200 ℃ and 5-10MPa, closing a gas channel after the reaction is finished, and cooling and carrying out solid-liquid separation to obtain carbonate minerals so as to realize carbon sequestration. |[0014] The elevation of the temperature within a certain range can improve the dissolution reaction activity of an alkalinity source in the mineral leaching suspension, accelerate the dissolution of calcium and magnesium ions, increase the concentration of the calcium and magnesium ions in the solution, thereby being beneficial to separating out calcium carbonate and magnesium carbonate and improving the carbonation conversion rate, however, excessive elevation of the temperature also can lead to the reduction of the solubility of carbon dioxide, and lead to the reduction of carbonate radical or bicarbonate radical ions in the solution, thereby being unfavorable for the forward progress of the precipitation reaction, therefore, the inventor controls the reaction temperature within 100-200 ℃ to ensure that the carbonation conversion rate of the carbonation reaction is maximum, and simultaneously has better carbon fixation effect, and better temperature control is 15-180 ℃ and is optimal. The pressure is also controlled within the carbonation conversion range, so that the dissolution of calcium and magnesium ions is accelerated, and more carbonate or bicarbonate ions are generated, so that the carbonation reaction is more efficient.|[0015] The acid liquor used in the acid leaching pretreatment is different according to the difference of alkalinity sources, and concretely comprises the following steps of pretreatment of olivine by sulfuric acid, pretreatment of basalt by hydrochloric acid, pretreatment of wollastonite by hydrochloric acid and pretreatment of anorthite by acetic acid.|[0016] Wherein, the pretreatment agent is different according to the difference of alkalinity sources, and the specific following steps are adopted:|[0017] The pretreatment agent added into the olivine and anorthite mineral leaching suspension under the condition of pH value of 10-11 is 0.50mol/L NaHCO 3 and 1.00mol/L NaCl; |[0018] under the condition of pH value of 10, adding a pretreatment agent which is 0.50mol/L NaHCO 3 into the basalt mineral leaching suspension; |[0019] The pretreatment agent added into the wollastonite mineral leaching suspension at the pH of 10 is 0.50mol/L NaHCO 3 and 0.25mol/L NaCl. |[0020] The NaHCO 3 is used for keeping the concentration of bicarbonate ions in the solution to be higher, and can well regulate pH change caused by dissolution of carbon dioxide while promoting the reaction, reduce the resistance in the formation process of calcium carbonate and magnesium carbonate, and the addition of NaCl can improve the solubility of silicate minerals, thereby promoting the leaching of calcium and magnesium ions and promoting the reaction. When NaHCO 3 and NaCl are mixed for use, the synergistic effect of the two components can further improve the carbonation conversion rate, mainly because NaCl is completely ionized in suspension, the salt ion effect is fully exerted, and the solubility of calcium carbonate is improved while the dissolution of wollastonite is promoted.|[0021] In addition, the mass ratio of the mineral leaching suspension to the pretreatment agent is controlled to be 10-20:1, and the increase of the liquid-solid ratio is not only beneficial to the dispersion of an alkalinity source, but also reduces the wrapping of the surface of the mineral by the generated carbonate mineral, so that the carbonation reaction efficiency is improved, and more carbonate minerals can be generated within a certain time.|[0022] Finally, it should be noted that the carbon dioxide gas of the present invention may originate from a carbon dioxide emission tower or other carbon dioxide emission points of a thermal power plant, such as a power plant, a metallurgical plant, an oil refinery, etc., where the carbon emission points preferably themselves generate alkalinity sources, especially mines, and surrounding rocks of many mining areas are such as olivine rocks and basalt rocks, while the downstream beneficiation metallurgical process has a large amount of carbon emission, and the two areas are generally very close together, so that the carbon emission of each process can be reduced, and the coal mine is also similar. The carbon emission is carried out, and meanwhile, the permanent sealing and storage of carbon dioxide are realized, so that the development goal of green low carbon is realized.|[0023] The technical scheme of the embodiment of the invention has at least the following advantages and beneficial effects:|[0024] 1. the method comprises the steps of sealing and storing carbon dioxide in a wet carbonation mode, carrying out acid leaching pretreatment on an alkalinity source before reaction, firstly dissolving out partial calcium and magnesium ions preferentially, avoiding that the calcium and magnesium ions migrate to the surface of the alkalinity source mineral in the reaction process to generate carbonate minerals so as to prevent the subsequent carbonation reaction from being carried out and affecting the sealing and storing effect, and carrying out carbonation reaction on the pretreated alkalinity source and the carbon dioxide to form stable carbonate minerals, thereby realizing the sealing and storing of the carbon. |[0025] 2. In the invention, different alkalinity sources are treated by different acids and then mixed with different pretreatment agents to obtain the pretreated alkalinity sources, so that the carbonation conversion rate is improved and the carbon sealing quantity is also improved in the carbonation reaction process, thereby realizing the permanent, stable and large-scale sealing of carbon dioxide.|INVENTION MODE|Detailed Description|[0026] In order to make the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention will be clearly and completely described below. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.|[0027] Example 1|[0028] A method for carbon sequestration using an alkalinity source comprising the steps of:|[0029] (1) Grinding and crushing an alkalinity source and screening the alkalinity source to obtain alkalinity source powder with the particle size of 38 mu m, wherein the alkalinity source comprises olivine, basalt, wollastonite and anorthite; |[0030] (2) Acid leaching is carried out on the alkalinity source powder, the liquid-solid ratio during acid leaching is 10:1mL/g, thus obtaining an ore leaching suspension, and then the ore leaching suspension and a pretreatment agent are mixed according to the mass ratio of 20:1 for reaction, thus obtaining a pretreatment alkalinity source; |[0031] wherein, during acid leaching, sulfuric acid is utilized to pretreat olivine, hydrochloric acid is utilized to pretreat basalt, hydrochloric acid is utilized to pretreat wollastonite, and acetic acid is utilized to pretreat anorthite; |[0032] the pretreatment agent is different according to the alkalinity sources, and the pretreatment agent is concretely as follows: |[0033] The pretreatment agent added into the olivine and anorthite mineral leaching suspension at pH 11 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 1.00 mol/L; |[0034] Under the condition of pH value of 10, adding a pretreatment agent of 0.50mol/L NaHCO 3 into the basalt mineral leaching suspension; |[0035] The pretreatment agent added into wollastonite mineral leaching suspension liquid under the condition of pH 10 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 0.25 mol/L; |[0036] (3) Mixing the pretreated alkalinity source and water according to the mass ratio of 1:20, adding into a reaction kettle, stirring for 10min at the stirring speed of 260r/min, then introducing carbon dioxide gas of a carbon dioxide discharge tower of a thermal power plant, performing carbonation reaction for 1h at the stirring speed of 240r/min under the conditions of 180 ℃ and 8MPa, closing a gas channel after the reaction is finished, and cooling and separating solid from liquid to obtain carbonate minerals, thereby realizing the carbon sequestration. |[0037] Example 2|[0038] A method for carbon sequestration using an alkalinity source comprising the steps of:|[0039] (1) Grinding and crushing an alkalinity source and screening the alkalinity source to obtain alkalinity source powder with the particle size of 33 mu m, wherein the alkalinity source comprises olivine, basalt, wollastonite and anorthite; |[0040] (2) Acid leaching is carried out on the alkalinity source powder, the liquid-solid ratio during acid leaching is 15:1mL/g, thus obtaining an ore leaching suspension, and then the ore leaching suspension and a pretreatment agent are mixed according to the mass ratio of 20:1 for reaction, thus obtaining a pretreatment alkalinity source; |[0041] wherein, during the acid leaching pretreatment, sulfuric acid is utilized to pretreat olivine, hydrochloric acid is utilized to pretreat basalt, hydrochloric acid is utilized to pretreat wollastonite, and acetic acid is utilized to pretreat anorthite; |[0042] the pretreatment agent is different according to the alkalinity sources, and the pretreatment agent is concretely as follows: |[0043] The pretreatment agent added into the olivine and anorthite mineral leaching suspension at pH of 10 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 1.00 mol/L; |[0044] Under the condition of pH value of 10, adding a pretreatment agent of 0.50mol/L NaHCO 3 into the basalt mineral leaching suspension; |[0045] The pretreatment agent added into wollastonite mineral leaching suspension liquid under the condition of pH 10 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 0.25 mol/L; |[0046] (3) Mixing the pretreated alkalinity source and water according to the mass ratio of 1:20, adding into a reaction kettle, stirring for 20min at the stirring speed of 200r/min, then introducing carbon dioxide gas of a carbon dioxide discharge tower of a thermal power plant, performing carbonation reaction for 1h at the stirring speed of 280r/min under the conditions of 120 ℃ and 6MPa, closing a gas channel after the reaction is finished, and cooling and separating solid from liquid to obtain carbonate minerals, thereby realizing the carbon sequestration. |[0047] Example 3|[0048] A method for carbon sequestration using an alkalinity source comprising the steps of:|[0049] (1) Grinding and crushing an alkalinity source and screening the alkalinity source to obtain alkalinity source powder with the particle size of 42 mu m, wherein the alkalinity source comprises olivine, basalt, wollastonite and anorthite; |[0050] (2) Acid leaching is carried out on the alkalinity source powder, the liquid-solid ratio during acid leaching is 10:1mL/g, thus obtaining an ore leaching suspension, and then the ore leaching suspension and a pretreatment agent are mixed according to the mass ratio of 20:1 for reaction, thus obtaining a pretreatment alkalinity source; |[0051] wherein, during the acid leaching pretreatment, sulfuric acid is utilized to pretreat olivine, hydrochloric acid is utilized to pretreat basalt, hydrochloric acid is utilized to pretreat wollastonite, and acetic acid is utilized to pretreat anorthite; |[0052] the pretreatment agent is different according to the alkalinity sources, and the pretreatment agent is concretely as follows: |[0053] The pretreatment agent added into the olivine and anorthite mineral leaching suspension at pH of 10.5 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 1.00 mol/L; |[0054] Under the condition of pH value of 10, adding a pretreatment agent of 0.50mol/L NaHCO 3 into the basalt mineral leaching suspension; |[0055] The pretreatment agent added into wollastonite mineral leaching suspension liquid under the condition of pH 10 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 0.25 mol/L; |[0056] (3) Mixing the pretreated alkalinity source and water according to the mass ratio of 1:20, adding into a reaction kettle, stirring for 5min at the stirring speed of 300r/min, then introducing carbon dioxide gas of a carbon dioxide discharge tower of a thermal power plant, performing carbonation reaction for 1h at the stirring speed of 200r/min and under the conditions of 160 ℃ and 7MPa, closing a gas channel after the reaction is finished, and cooling and separating solid from liquid to obtain carbonate minerals, thereby realizing the carbon sequestration. |[0057] Comparative example 1|[0058] The comparative example differs from example 1 in that step (2) was not included.|[0059] Comparative example 2|[0060] This comparative example differs from example 1 in that in step (2), the alkalinity source powder is not subjected to acid leaching treatment.|[0061] Comparative example 3|[0062] This comparative example differs from example 1 in that in step (2) the mineral leaching suspension is not reacted with the pretreatment agent.|[0063] Experimental example|[0064] 1. The carbonation conversion and carbon sequestration amount in each example and comparative example were separately tested and the test results are shown in Table 1, wherein the carbonation conversion was measured by measuring the initial amount of CO 2 before the reaction (gas chromatography), filtering the solid product after the reaction, measuring the amount of CO 2 released after acidolysis (hydrochloric acid titration), the conversion = (reaction consumed CO 2 amount/initial CO 2 amount) x 100%, and the carbon sequestration amount was measured by measuring the total amount of carbonate in the product by chemical analysis, converting to CO 2 sequestration amount in combination with molar mass, specifically by extracting and purifying the carbonate product, and calculating the corresponding amount of CO 2 by stoichiometric relation.|[0065] Table 1-test results for each example and comparative example|[0066] Carbonation conversion (%)Carbon inventory (mol/kg)Example 191.59.23Example 290.89.20Example 391.29.21Comparative example 158.65.2Comparative example 236.23.1Comparative example 325.72.4|[0067] The results in table 1 show that the method comprises the steps of firstly carrying out acid leaching pretreatment on the alkalinity source before reaction, firstly dissolving out part of calcium and magnesium ions preferentially, and then carbonating the pretreated alkalinity source with carbon dioxide, so that the carbon is stored, more importantly, the carbonation conversion rate and the carbon storage quantity are improved, carbonate minerals are prevented from being generated by migration of the calcium and magnesium ions to the surfaces of the minerals in the carbonation reaction process of the alkalinity source and the carbon dioxide, and the part of carbonate minerals can wrap the minerals to hinder the carbonation reaction, so that the storage effect is affected.|[0068] The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention. (CN120242698)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of carbon dioxide sealing and storage, in particular to a method for realizing carbon sealing and storage by utilizing an alkalinity source.|BACKGROUND ART|[0002] As the greenhouse gas content in the atmosphere gradually increases, the global climate changes significantly and the atmospheric concentration of carbon dioxide increases significantly.|[0003] At present, the internationally common carbon dioxide control technology mainly comprises three steps of (1) reducing the use of non-renewable energy sources such as fossil fuel (coal, petroleum and natural gas), developing and utilizing renewable energy sources such as geothermal energy, wind energy and biomass energy, reducing the occupation ratio of primary energy consumption by changing an energy structure, (2) improving the energy conversion efficiency, advocating green and energy-saving life, and (3) adopting a carbon dioxide capturing and sealing technology (CCS). Among them, CCS technology is considered as one of the most promising technologies for solving the greenhouse effect, and has a certain feasibility in the treatment of large-scale carbon dioxide sources.|[0004] The carbon dioxide sealing mode mainly comprises geological sealing, mineral sealing and marine sealing, wherein the geological sealing is to pour carbon dioxide into a proper stratum under pressure, the carbon dioxide is stored in the pore space of the stratum, the mineral sealing is to enable the carbon dioxide to chemically react with metal oxide to form carbonate and other byproducts in solid forms, and the marine sealing is to pour liquid carbon dioxide into a deep sea water area to form a stable lake-shaped structure under high-pressure conditions.|[0005] The mineral sealing and storage method utilizes the chemical reaction of carbon dioxide and certain minerals (such as olivine) to generate stable carbonate minerals, and the sealing and storage method is stable and has no leakage risk. And most of carbon on the earth exists in the form of carbonate minerals, and carbon sequestration in the crystal structure of the minerals is a long-lasting and reliable method, so carbon dioxide mineral sequestration is acknowledged as the safest and reliable sequestration method.|[0006] Based on this, when carbon dioxide is sequestered, if dry carbonation is adopted, that is, carbonate is obtained directly by using a gas-solid one-step reaction mode, but the method needs to be carried out at high temperature and high pressure to isolate carbon dioxide from the atmosphere, however, one major disadvantage of the method is that the reaction kinetics of calcium silicate and magnesium silicate are often too slow, and the acceleration of the reaction kinetics by increasing the temperature is often thermodynamically limited. It is therefore important to find a suitable and stable wet carbonation for carbon dioxide sequestration.|DISCLOSURE|Disclosure of Invention|[0007] Based on the above problems, it is an object of the present invention to provide a method for carbon sequestration using an alkalinity source which allows permanent, stable and large scale sequestration of carbon dioxide.|[0008] The inventor seeks to sequester carbon dioxide in a wet carbonation manner, however, in research and practice the inventor has found that calcium and magnesium ions migrate to the surface of the mineral during the reaction to form carbonate minerals, which encapsulate the mineral and hinder the carbonation reaction and thus affect the sequestering effect. Therefore, the method comprises the steps of firstly carrying out acid leaching pretreatment on an alkalinity source before reaction, firstly dissolving out partial calcium and magnesium ions preferentially, then carbonating the pretreated alkalinity source with carbon dioxide, dissolving the carbon dioxide in a liquid phase to generate carbonic acid, decomposing the carbonic acid into carbonate ions or bicarbonate ions, dissolving out metal ions by the alkalinity source under the proton exchange effect, and carrying out chemical precipitation with the carbonic acid decomposed carbonate ions or bicarbonate ions to form stable carbonate rock mineral, thereby realizing the carbon sequestration.|[0009] The implementation mode of the invention is realized by the following technical scheme:|[0010] a method for carbon sequestration using an alkalinity source comprising the steps of: |[0011] (1) Grinding and crushing an alkalinity source and screening the alkalinity source to the particle size of 30-50 mu m to obtain alkalinity source powder, wherein the alkalinity source comprises olivine, basalt, wollastonite, anorthite and the like; |[0012] (2) Acid leaching is carried out on the alkalinity source powder, the liquid-solid ratio during acid leaching is 10-20:1mL/g, thus obtaining an ore leaching suspension, and then the ore leaching suspension and a pretreatment agent are mixed according to the mass ratio of 10-20:1 for reaction, thus obtaining a pretreatment alkalinity source; |[0013] (3) Mixing a pretreated alkalinity source and water according to a mass ratio of 1:10-20, adding the mixture into a reaction kettle, stirring the mixture for 5-20min at a stirring speed of 200-300r/min, then introducing carbon dioxide gas, wherein the carbon dioxide gas can be sourced from a carbon dioxide discharge tower or other carbon dioxide discharge towers of a thermal power plant, and carrying out carbonation reaction for 0.5-1.5h at a stirring speed of 200-300r/min under the conditions of 100-200 ℃ and 5-10MPa, closing a gas channel after the reaction is finished, and cooling and carrying out solid-liquid separation to obtain carbonate minerals so as to realize carbon sequestration. |[0014] The elevation of the temperature within a certain range can improve the dissolution reaction activity of an alkalinity source in the mineral leaching suspension, accelerate the dissolution of calcium and magnesium ions, increase the concentration of the calcium and magnesium ions in the solution, thereby being beneficial to separating out calcium carbonate and magnesium carbonate and improving the carbonation conversion rate, however, excessive elevation of the temperature also can lead to the reduction of the solubility of carbon dioxide, and lead to the reduction of carbonate radical or bicarbonate radical ions in the solution, thereby being unfavorable for the forward progress of the precipitation reaction, therefore, the inventor controls the reaction temperature within 100-200 ℃ to ensure that the carbonation conversion rate of the carbonation reaction is maximum, and simultaneously has better carbon fixation effect, and better temperature control is 15-180 ℃ and is optimal. The pressure is also controlled within the carbonation conversion range, so that the dissolution of calcium and magnesium ions is accelerated, and more carbonate or bicarbonate ions are generated, so that the carbonation reaction is more efficient.|[0015] The acid liquor used in the acid leaching pretreatment is different according to the difference of alkalinity sources, and concretely comprises the following steps of pretreatment of olivine by sulfuric acid, pretreatment of basalt by hydrochloric acid, pretreatment of wollastonite by hydrochloric acid and pretreatment of anorthite by acetic acid.|[0016] Wherein, the pretreatment agent is different according to the difference of alkalinity sources, and the specific following steps are adopted:|[0017] The pretreatment agent added into the olivine and anorthite mineral leaching suspension under the condition of pH value of 10-11 is 0.50mol/L NaHCO 3 and 1.00mol/L NaCl; |[0018] under the condition of pH value of 10, adding a pretreatment agent which is 0.50mol/L NaHCO 3 into the basalt mineral leaching suspension; |[0019] The pretreatment agent added into the wollastonite mineral leaching suspension at the pH of 10 is 0.50mol/L NaHCO 3 and 0.25mol/L NaCl. |[0020] The NaHCO 3 is used for keeping the concentration of bicarbonate ions in the solution to be higher, and can well regulate pH change caused by dissolution of carbon dioxide while promoting the reaction, reduce the resistance in the formation process of calcium carbonate and magnesium carbonate, and the addition of NaCl can improve the solubility of silicate minerals, thereby promoting the leaching of calcium and magnesium ions and promoting the reaction. When NaHCO 3 and NaCl are mixed for use, the synergistic effect of the two components can further improve the carbonation conversion rate, mainly because NaCl is completely ionized in suspension, the salt ion effect is fully exerted, and the solubility of calcium carbonate is improved while the dissolution of wollastonite is promoted.|[0021] In addition, the mass ratio of the mineral leaching suspension to the pretreatment agent is controlled to be 10-20:1, and the increase of the liquid-solid ratio is not only beneficial to the dispersion of an alkalinity source, but also reduces the wrapping of the surface of the mineral by the generated carbonate mineral, so that the carbonation reaction efficiency is improved, and more carbonate minerals can be generated within a certain time.|[0022] Finally, it should be noted that the carbon dioxide gas of the present invention may originate from a carbon dioxide emission tower or other carbon dioxide emission points of a thermal power plant, such as a power plant, a metallurgical plant, an oil refinery, etc., where the carbon emission points preferably themselves generate alkalinity sources, especially mines, and surrounding rocks of many mining areas are such as olivine rocks and basalt rocks, while the downstream beneficiation metallurgical process has a large amount of carbon emission, and the two areas are generally very close together, so that the carbon emission of each process can be reduced, and the coal mine is also similar. The carbon emission is carried out, and meanwhile, the permanent sealing and storage of carbon dioxide are realized, so that the development goal of green low carbon is realized.|[0023] The technical scheme of the embodiment of the invention has at least the following advantages and beneficial effects:|[0024] 1. the method comprises the steps of sealing and storing carbon dioxide in a wet carbonation mode, carrying out acid leaching pretreatment on an alkalinity source before reaction, firstly dissolving out partial calcium and magnesium ions preferentially, avoiding that the calcium and magnesium ions migrate to the surface of the alkalinity source mineral in the reaction process to generate carbonate minerals so as to prevent the subsequent carbonation reaction from being carried out and affecting the sealing and storing effect, and carrying out carbonation reaction on the pretreated alkalinity source and the carbon dioxide to form stable carbonate minerals, thereby realizing the sealing and storing of the carbon. |[0025] 2. In the invention, different alkalinity sources are treated by different acids and then mixed with different pretreatment agents to obtain the pretreated alkalinity sources, so that the carbonation conversion rate is improved and the carbon sealing quantity is also improved in the carbonation reaction process, thereby realizing the permanent, stable and large-scale sealing of carbon dioxide.|INVENTION MODE|Detailed Description|[0026] In order to make the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention will be clearly and completely described below. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.|[0027] Example 1|[0028] A method for carbon sequestration using an alkalinity source comprising the steps of:|[0029] (1) Grinding and crushing an alkalinity source and screening the alkalinity source to obtain alkalinity source powder with the particle size of 38 mu m, wherein the alkalinity source comprises olivine, basalt, wollastonite and anorthite; |[0030] (2) Acid leaching is carried out on the alkalinity source powder, the liquid-solid ratio during acid leaching is 10:1mL/g, thus obtaining an ore leaching suspension, and then the ore leaching suspension and a pretreatment agent are mixed according to the mass ratio of 20:1 for reaction, thus obtaining a pretreatment alkalinity source; |[0031] wherein, during acid leaching, sulfuric acid is utilized to pretreat olivine, hydrochloric acid is utilized to pretreat basalt, hydrochloric acid is utilized to pretreat wollastonite, and acetic acid is utilized to pretreat anorthite; |[0032] the pretreatment agent is different according to the alkalinity sources, and the pretreatment agent is concretely as follows: |[0033] The pretreatment agent added into the olivine and anorthite mineral leaching suspension at pH 11 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 1.00 mol/L; |[0034] Under the condition of pH value of 10, adding a pretreatment agent of 0.50mol/L NaHCO 3 into the basalt mineral leaching suspension; |[0035] The pretreatment agent added into wollastonite mineral leaching suspension liquid under the condition of pH 10 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 0.25 mol/L; |[0036] (3) Mixing the pretreated alkalinity source and water according to the mass ratio of 1:20, adding into a reaction kettle, stirring for 10min at the stirring speed of 260r/min, then introducing carbon dioxide gas of a carbon dioxide discharge tower of a thermal power plant, performing carbonation reaction for 1h at the stirring speed of 240r/min under the conditions of 180 ℃ and 8MPa, closing a gas channel after the reaction is finished, and cooling and separating solid from liquid to obtain carbonate minerals, thereby realizing the carbon sequestration. |[0037] Example 2|[0038] A method for carbon sequestration using an alkalinity source comprising the steps of:|[0039] (1) Grinding and crushing an alkalinity source and screening the alkalinity source to obtain alkalinity source powder with the particle size of 33 mu m, wherein the alkalinity source comprises olivine, basalt, wollastonite and anorthite; |[0040] (2) Acid leaching is carried out on the alkalinity source powder, the liquid-solid ratio during acid leaching is 15:1mL/g, thus obtaining an ore leaching suspension, and then the ore leaching suspension and a pretreatment agent are mixed according to the mass ratio of 20:1 for reaction, thus obtaining a pretreatment alkalinity source; |[0041] wherein, during the acid leaching pretreatment, sulfuric acid is utilized to pretreat olivine, hydrochloric acid is utilized to pretreat basalt, hydrochloric acid is utilized to pretreat wollastonite, and acetic acid is utilized to pretreat anorthite; |[0042] the pretreatment agent is different according to the alkalinity sources, and the pretreatment agent is concretely as follows: |[0043] The pretreatment agent added into the olivine and anorthite mineral leaching suspension at pH of 10 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 1.00 mol/L; |[0044] Under the condition of pH value of 10, adding a pretreatment agent of 0.50mol/L NaHCO 3 into the basalt mineral leaching suspension; |[0045] The pretreatment agent added into wollastonite mineral leaching suspension liquid under the condition of pH 10 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 0.25 mol/L; |[0046] (3) Mixing the pretreated alkalinity source and water according to the mass ratio of 1:20, adding into a reaction kettle, stirring for 20min at the stirring speed of 200r/min, then introducing carbon dioxide gas of a carbon dioxide discharge tower of a thermal power plant, performing carbonation reaction for 1h at the stirring speed of 280r/min under the conditions of 120 ℃ and 6MPa, closing a gas channel after the reaction is finished, and cooling and separating solid from liquid to obtain carbonate minerals, thereby realizing the carbon sequestration. |[0047] Example 3|[0048] A method for carbon sequestration using an alkalinity source comprising the steps of:|[0049] (1) Grinding and crushing an alkalinity source and screening the alkalinity source to obtain alkalinity source powder with the particle size of 42 mu m, wherein the alkalinity source comprises olivine, basalt, wollastonite and anorthite; |[0050] (2) Acid leaching is carried out on the alkalinity source powder, the liquid-solid ratio during acid leaching is 10:1mL/g, thus obtaining an ore leaching suspension, and then the ore leaching suspension and a pretreatment agent are mixed according to the mass ratio of 20:1 for reaction, thus obtaining a pretreatment alkalinity source; |[0051] wherein, during the acid leaching pretreatment, sulfuric acid is utilized to pretreat olivine, hydrochloric acid is utilized to pretreat basalt, hydrochloric acid is utilized to pretreat wollastonite, and acetic acid is utilized to pretreat anorthite; |[0052] the pretreatment agent is different according to the alkalinity sources, and the pretreatment agent is concretely as follows: |[0053] The pretreatment agent added into the olivine and anorthite mineral leaching suspension at pH of 10.5 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 1.00 mol/L; |[0054] Under the condition of pH value of 10, adding a pretreatment agent of 0.50mol/L NaHCO 3 into the basalt mineral leaching suspension; |[0055] The pretreatment agent added into wollastonite mineral leaching suspension liquid under the condition of pH 10 is NaHCO 3 with the concentration of 0.50mol/L and NaCl with the concentration of 0.25 mol/L; |[0056] (3) Mixing the pretreated alkalinity source and water according to the mass ratio of 1:20, adding into a reaction kettle, stirring for 5min at the stirring speed of 300r/min, then introducing carbon dioxide gas of a carbon dioxide discharge tower of a thermal power plant, performing carbonation reaction for 1h at the stirring speed of 200r/min and under the conditions of 160 ℃ and 7MPa, closing a gas channel after the reaction is finished, and cooling and separating solid from liquid to obtain carbonate minerals, thereby realizing the carbon sequestration. |[0057] Comparative example 1|[0058] The comparative example differs from example 1 in that step (2) was not included.|[0059] Comparative example 2|[0060] This comparative example differs from example 1 in that in step (2), the alkalinity source powder is not subjected to acid leaching treatment.|[0061] Comparative example 3|[0062] This comparative example differs from example 1 in that in step (2) the mineral leaching suspension is not reacted with the pretreatment agent.|[0063] Experimental example|[0064] 1. The carbonation conversion and carbon sequestration amount in each example and comparative example were separately tested and the test results are shown in Table 1, wherein the carbonation conversion was measured by measuring the initial amount of CO 2 before the reaction (gas chromatography), filtering the solid product after the reaction, measuring the amount of CO 2 released after acidolysis (hydrochloric acid titration), the conversion = (reaction consumed CO 2 amount/initial CO 2 amount) x 100%, and the carbon sequestration amount was measured by measuring the total amount of carbonate in the product by chemical analysis, converting to CO 2 sequestration amount in combination with molar mass, specifically by extracting and purifying the carbonate product, and calculating the corresponding amount of CO 2 by stoichiometric relation.|[0065] Table 1-test results for each example and comparative example|[0066] Carbonation conversion (%)Carbon inventory (mol/kg)Example 191.59.23Example 290.89.20Example 391.29.21Comparative example 158.65.2Comparative example 236.23.1Comparative example 325.72.4|[0067] The results in table 1 show that the method comprises the steps of firstly carrying out acid leaching pretreatment on the alkalinity source before reaction, firstly dissolving out part of calcium and magnesium ions preferentially, and then carbonating the pretreated alkalinity source with carbon dioxide, so that the carbon is stored, more importantly, the carbonation conversion rate and the carbon storage quantity are improved, carbonate minerals are prevented from being generated by migration of the calcium and magnesium ions to the surfaces of the minerals in the carbonation reaction process of the alkalinity source and the carbon dioxide, and the part of carbonate minerals can wrap the minerals to hinder the carbonation reaction, so that the storage effect is affected.|[0068] The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention. Family Number|(115152801)|115152801|Abstract|(CN120242698 A)|The invention provides a method for realizing carbon sequestration by using an alkalinity source , which comprises the following steps : ( 1 ) grinding , crushing and screening the alkalinity source to obtain alkalinity source powder ; wherein the alkalinity source is prepared from peridotite , basalt , wollastonite and anorthite ; ( 2 ) carrying out acid leaching on the alkalinity source powder to obtain an ore leaching suspension ; reacting the mineral leaching suspension liquid with a pretreatment agent under the conditions that the temperature is 150 DEG C , the pressure is 5 MPa and the liquid - solid ratio is 20 : 1 to obtain a pretreated alkalinity source ; ( 3 ) mixing the pretreated alkalinity source with water , and then introducing carbon dioxide gas to carry out carbonation reaction ; after the reaction is finished , a gas channel is closed , and carbonate rock minerals are obtained after cooling and solid - liquid separation , so that carbon sequestration is realized , and permanent , stable and large - scale sequestration of carbon dioxide can be realized . |CPC codes|(CN120242698 A)|B01D - 053/62 |B01D - 053/78 |B01D - 2251/304 |B01D - 2251/402 |B01D - 2251/404 |B01D - 2251/604 |B01D - 2257/504 |B01D - 2258/0283 |C01B - 032/60 |C01F - 005/24 |C01F - 011/18/1 |C01F - 011/18 |IPC codes|(CN120242698 A)|B01D - 053/34 |B01D - 053/62 |B01D - 053/78 |C01F - 011/18 |Title|(CN120242698 A)|Method for realizing carbon sequestration by using alkalinity source | Environmental technology|Materials, metallurgy B01D-053/62|B01D-053/78|B01D-2251/304|B01D-2251/402|B01D-2251/404|B01D-2251/604|B01D-2257/504|B01D-2258/0283|C01B-032/60|C01F-005/24|C01F-011/18|C01F-011/18/1|Y02A-050/2342|Y02C-010/04|Y02C-010/06|Y02P-020/152 B01D-053/62|B01D-053/78|B01D-2251/304|B01D-2251/402|B01D-2251/404|B01D-2251/604|B01D-2257/504|B01D-2258/0283|C01B-032/60|C01F-005/24|C01F-011/18|C01F-011/18/1|Y02A-050/2342|Y02C-010/04|Y02C-010/06|Y02P-020/152 B01D-053/34|B01D-053/62|B01D-053/78|C01F-011/18 B01D-053/34|B01D-053/62|B01D-053/78|C01F-011/18 PENDING (CN120242698)|PENDING ALIVE (CN120242698)|ALIVE (CN120242698)|LEGAL DETAILS FOR CN120242698|Actual or expected expiration date=2045-04-02|Legal state=ALIVE|Status=PENDING|Event publication date=2025-04-02|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510409398|Application date=2025-04-02|Standardized application number=2025CN-0409398|Event publication date=2025-07-04|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120242698|Publication stage code=A|Publication date=2025-07-04|Standardized publication number=CN120242698|Event publication date=2025-07-04|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-07-22|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN120242698)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfm21EzaCNDslfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=JTq4%252BgOBgHG7JUOltU5EE5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN120242698)|CN (CN120242698)|NAME=JIANGXI UNIVERSITY OF SCIENCE & TECHONOLOGY , COUNTRY=CN (CN120242698)|NAME=LIU JINRONG;CHENGDU RUI DAO ZHICHENG PATENT AGENCY CO., LTD. , REG=51217 (CN120242698)|CN (CN120242698)|NAME=HE YANXIN, COUNTRY=CN |NAME=WANG LISHUANG|NAME=WEI MINGCONG|NAME=DENG ZHAOSHAN 0 1 Titre: (CN120242698)|Method for realizing carbon sequestration by using alkalinity source Résumé: (CN120242698)|The invention provides a method for realizing carbon sequestration by using an alkalinity source, which comprises the following steps: (1) grinding, crushing and screening the alkalinity source to obtain alkalinity source powder; wherein the alkalinity source is prepared from peridotite, basalt, wollastonite and anorthite; (2) carrying out acid leaching on the alkalinity source powder to obtain an ore leaching suspension; reacting the mineral leaching suspension liquid with a pretreatment agent under the conditions that the temperature is 150 DEG C, the pressure is 5MPa and the liquid-solid ratio is 20: 1 to obtain a pretreated alkalinity source; (3) mixing the pretreated alkalinity source with water, and then introducing carbon dioxide gas to carry out carbonation reaction; after the reaction is finished, a gas channel is closed, and carbonate rock minerals are obtained after cooling and solid-liquid separation, so that carbon sequestration is realized, and permanent, stable and large-scale sequestration of carbon dioxide can be realized. 39 Abstract gpt-4o-mini yes The method explicitly describes the use of alkalinity sources (peridotite, basalt) for carbon sequestration through mineral carbonation, which aligns with the topic of enhanced weathering.
41 CN202421798515U CN202421798515U CN222852656 114517722 CN222852656 U 2025-05-13 [CN222852656U] 2024-07-29 2024-07-29 2025-05-13 (CN222852656U)|2025-05-13 (CN222852656)|2034-07-29 (CN222852656)|Soil carbon sequestration improvement device (CN222852656)|The utility model provides an improved soil carbon sequestration device, which relates to the technical field of soil carbon sequestration devices and comprises a stirring and mixing tank, a tank cover is mounted at the top of the stirring and mixing tank, a feeding port is connected to the top of the tank cover, a rotating motor is mounted on the side face of the feeding port, one end of the rotating motor is connected with a rotating shaft, and the other end of the rotating shaft is connected with a rotating shaft. A plurality of crushing cutters are distributed on the outer side of the rotating shaft, a stirring motor is mounted at the top of the tank cover, a transmission shaft is connected to the bottom of the stirring motor, and a plurality of stirring sticks are distributed on the outer side of the transmission shaft. According to the device, the rotating shaft is electrically driven to rotate through the rotating motor, so that the rotating shaft drives the crushing cutters to rotate, the crushing cutters can scatter caked soil, soil pores can be increased, the soil structure becomes loose, the soil and an organic fertilizer can be fully and uniformly mixed, and the soil and the organic fertilizer can be uniformly mixed. The condition of non-uniform mixing of the organic fertilizer is avoided, the soil quality is improved, and the soil carbon sequestration effect is further improved. FUJIAN DUNFENG TANHUI AGRICULTURAL TECHNOLOGY (CN222852656)|FUJIAN DUNFENG TANHUI AGRICULTURAL TECHNOLOGY CO., LTD. ([CN]) KANG QUAN|KANG XIAOXIONG (CN222852656)|KANG QUAN|KANG XIAOXIONG (CN222852656)|LIU YONGQING;BEIJING DAWSON ZHIGU INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) et al.|Reg. Nb: 33468 (CN222852656)|Compared with the prior art, the utility model has the advantages and positive effects that,|In the prior art, in the stage of soil carbon fixation improvement, the soil and the organic fertilizer are required to be mixed, so that the organic carbon content in the soil is improved, but the existing soil is seriously agglomerated and is difficult to uniformly mix with the organic fertilizer, so that the soil carbon fixation effect is insufficient, and the problem of reduction of the soil improvement effect is caused.Disclosure of utility modelThe utility model aims to solve the problems that in the prior art, soil is seriously agglomerated and is difficult to uniformly mix with an organic fertilizer, so that the soil carbon fixation effect is insufficient, and the soil improvement effect is reduced.| (CN222852656)|1. The utility model provides a soil solid carbon improvement device, includes stirring blending tank (1), wherein, tank cover (2) are installed at the top of stirring blending tank (1), the top of tank cover (2) is connected with feed inlet (3), rotation motor (4) are installed to the side-mounting of feed inlet (3), the one end of rotation motor (4) is connected with axis of rotation (5), the outside of axis of rotation (5) distributes and has a plurality of crushing sword (6), agitator motor (7) are installed at the top of tank cover (2), the bottom of agitator motor (7) is connected with transmission shaft (8), the outside of transmission shaft (8) distributes and has a plurality of stirring rod (9).| (CN222852656)|The utility model provides a soil carbon fixing improvement device, which relates to the technical field of soil carbon fixing devices and comprises a stirring and mixing tank, wherein a tank cover is arranged at the top of the stirring and mixing tank, a feed inlet is connected to the top of the tank cover, a rotating motor is arranged on the side surface of the feed inlet, one end of the rotating motor is connected with a rotating shaft, a plurality of crushing cutters are distributed on the outer side of the rotating shaft, a stirring motor is arranged at the top of the tank cover, a transmission shaft is connected to the bottom of the stirring motor, and a plurality of stirring rods are distributed on the outer side of the transmission shaft. According to the utility model, the rotating shaft is driven to rotate by the motor, so that the rotating shaft drives the crushing cutter to rotate, the crushing cutter is beneficial to scattering soil of a block, the pores of the soil are increased, the soil structure is loosened, the soil and the organic fertilizer are fully and uniformly mixed, the condition of uneven mixing of the organic fertilizer is avoided, the soil quality is improved, and the soil carbon fixation effect is further improved.| (CN222852656)|GROUND(100,24)|SOIL CARBON FIXATION(100,9)|STIRRING BLENDING TANK(100,3)|SOLID CARBON(100,1)|CRUSHING CUTTER(97,8)|CRUSHING SWORD(92,1)|SOIL CARBON SEQUESTRATION(71,14)|TANK COVER(65,13)|AGITATOR MOTOR(63,2)|THE(58,1)|FEED INLET(51,10)|MIXING TANK(45,17)|PACKING AUGER(43,5)|ORGANIC FERTILIZER(42,10)|ORGANIC FERTILIZER UNEVEN MIXING(42,2)|BLANK PIPE(39,4)|ROTATION MOTOR(37,2)|STIRRING MOTOR(36,9)|UNEVEN MIXING(36,2)|ROTATING MOTOR(30,7)|SOIL CARBON FIXING(30,2)|SOIL IMPROVEMENT(29,2)|BLOCK SOIL(26,2)|STIRRING ROD(25,8)|STIRRING TANK MIX(25,2)|SOIL IMPROVEMENT REDUCTION(25,1)|TRANSMISSION SHAFT(23,13)|ROTATING SHAFT(23,10)|FLUSHING PIPE BOTTOM(23,1)|SOIL CARBON(22,4)|SOIL QUALITY(18,2)|CONVEYER PIPE(14,5)|BLANKING PIPE INNER WALL(14,1)|ORGANIC CARBON CONTENT(13,2)|CONVEYING PIPE TOP(12,3)|WATERING FRAME TOP(12,2)|FEED PIPE(11,3)|STIRRING BOTTOM(11,3)|ORGANIC FERTILIZER BOX TOP(10,2)|BARREN DESERTIFICATION(10,1)|CONNECTING PIPE(9,8)|SOIL STRUCTURE(9,2)|WATER TANK(8,8)|SUPPORTING FRAME(8,7)|SOIL HOMOGENEITY(8,1)|DISCHARGE PIPE(7,2)|CAKING SOIL(7,1)|CONVEYING PIPE MIDDLE(7,1)|SOIL MICROBIAL REDUCTION(7,1)|WATERING FRAME SHOWER NOZZLE(7,1)|WATERING RACK(7,1)|SUPPORTING BLOCK BOTTOM(6,3)|PACKING AUGER OUTER SIDE(6,2)|POURING SOIL(6,1)|SCRAPER BLADE(6,1)|SOIL CARBON SEQUESTRATION CAPACITY(6,1)|STABLE CARBONACEOUS COMPOUND(6,1)|STIR SOIL(6,1)|OUTER SIDE(5,10)|SCRAPER PLATE(5,2)|TECHNICAL CONTENT(5,2)|DRIVE BROKEN SWORD(4,1)|INSIDE FERTILIZER(4,1)|RESIDUAL MATTER(4,1)|SOIL CARBON CONTENT(4,1)|TECHNICAL SUBSTANCE(4,1)| (CN222852656)|1. The utility model provides a soil solid carbon improvement device, includes stirring blending tank (1), wherein, tank cover (2) are installed at the top of stirring blending tank (1), the top of tank cover (2) is connected with feed inlet (3), rotation motor (4) are installed to the side-mounting of feed inlet (3), the one end of rotation motor (4) is connected with axis of rotation (5), the outside of axis of rotation (5) distributes and has a plurality of crushing sword (6), agitator motor (7) are installed at the top of tank cover (2), the bottom of agitator motor (7) is connected with transmission shaft (8), the outside of transmission shaft (8) distributes and has a plurality of stirring rod (9).|2. The soil carbon sequestration improvement device of claim 1, wherein a flushing pipe (16) is installed on the inner side of the stirring and mixing tank (1), a plurality of high-pressure nozzles are distributed on the bottom of the flushing pipe (16), a connecting pipe (17) is connected to the side surface of the flushing pipe (16), a pump (18) is connected to one end of the connecting pipe (17), and a water tank (19) is installed on the bottom of the pump (18).|3. The soil carbon sequestration improvement device of claim 1, wherein one end of the stirring rod (9) is connected with a scraper (10), the bottom of the transmission shaft (8) is connected with a packing auger (11), the bottom of the stirring and mixing tank (1) is connected with a blanking pipe (21), and the outer side of the packing auger (11) is connected with the inner wall of the blanking pipe (21).|4. The soil carbon sequestration improvement device of claim 1, wherein the stirring mixing tank (1) is internally provided with a watering frame (15), the top of the watering frame (15) is connected with a conveying pipe (13), the top of the conveying pipe (13) is connected with an organic fertilizer box (12), and the middle part of the conveying pipe (13) is provided with a valve (14).|5. The device for improving carbon sequestration of soil of claim 4, wherein the top of the organic fertilizer box (12) is connected with a feed pipe, a supporting block is installed at the bottom of the organic fertilizer box (12), and the bottom of the supporting block is connected with the top of the tank cover (2).|6. The soil carbon sequestration improvement apparatus as claimed in claim 2, characterized in that the outside of the stirring and mixing tank (1) is provided with a supporting frame (20), and the bottom of the water tank (19) is connected with the top of the supporting frame (20). (CN222852656)|TECHNICAL FIELD|Technical Field|[0001] The utility model relates to the technical field of soil carbon fixing devices, in particular to a soil carbon fixing improvement device.|BACKGROUND ART|[0002] Carbon sequestration in soil is one of means for reducing carbon emissions by combining carbon dioxide already present in the atmosphere and then converting it into a stable carbonaceous compound and storing it in the soil for a long period of time, and the organic carbon content and sequestration capacity in the soil are closely related to the fertility of the soil and crop yield, so that for poor soil with barren desertification, microbial reduction of the soil, and massive loss of organic carbon in the soil, carbon sequestration improvement by technical means is required to improve the carbon sequestration capacity of the soil.|[0003] In the prior art, in the stage of soil carbon fixation improvement, the soil and the organic fertilizer are required to be mixed, so that the organic carbon content in the soil is improved, but the existing soil is seriously agglomerated and is difficult to uniformly mix with the organic fertilizer, so that the soil carbon fixation effect is insufficient, and the problem of reduction of the soil improvement effect is caused.|DISCLOSURE|Disclosure of utility model|[0004] The utility model aims to solve the problems that in the prior art, soil is seriously agglomerated and is difficult to uniformly mix with an organic fertilizer, so that the soil carbon fixation effect is insufficient, and the soil improvement effect is reduced.|[0005] In order to achieve the purpose, the soil carbon fixation improvement device comprises a stirring and mixing tank, wherein a tank cover is arranged at the top of the stirring and mixing tank, a feed inlet is connected to the top of the tank cover, a rotating motor is arranged on the side face of the feed inlet, one end of the rotating motor is connected with a rotating shaft, a plurality of crushing cutters are distributed on the outer side of the rotating shaft, a stirring motor is arranged at the top of the tank cover, a transmission shaft is connected to the bottom of the stirring motor, and a plurality of stirring rods are distributed on the outer side of the transmission shaft.|[0006] Preferably, a flushing pipe is arranged on the inner side of the stirring and mixing tank, a plurality of high-pressure nozzles are distributed at the bottom of the flushing pipe, a connecting pipe is connected to the side face of the flushing pipe, a pump is connected to one end of the connecting pipe, and a water tank is arranged at the bottom of the pump.|[0007] Preferably, one end of the stirring rod is connected with a scraping plate, the bottom of the transmission shaft is connected with a packing auger, the bottom of the stirring and mixing tank is connected with a discharging pipe, and the outer side of the packing auger is connected with the inner wall of the discharging pipe.|[0008] Preferably, the internally mounted of stirring blending tank has the watering frame, the top of watering frame is connected with the conveyer pipe, the top of conveyer pipe is connected with the fertilizer case, the middle part of conveyer pipe is provided with the valve.|[0009] Preferably, the top of the organic fertilizer box is connected with a feeding pipe, a supporting block is arranged at the bottom of the organic fertilizer box, and the bottom of the supporting block is connected with the top of the tank cover.|[0010] Preferably, a supporting frame is arranged on the outer side of the stirring and mixing tank, and the bottom of the water tank is connected with the top of the supporting frame.|[0011] Compared with the prior art, the utility model has the advantages and positive effects that,|[0012] 1. According to the utility model, the rotating shaft is driven to rotate by the motor, so that the rotating shaft drives the crushing cutter to rotate, the crushing cutter is beneficial to scattering soil of a block, the pore space of the soil is increased, the soil structure is loosened, the soil and the organic fertilizer are fully and uniformly mixed, the condition of uneven mixing of the organic fertilizer is avoided, the soil quality is improved, and the soil carbon fixation effect is further improved.|[0013] 2. According to the utility model, the water source in the water tank is pumped by the pump, the water source is conveyed into the flushing pipe through the connecting pipe, and finally the water source is sprayed out through the high-pressure nozzles distributed at the bottom of the flushing pipe, so that the inner wall of the stirring and mixing tank is effectively flushed under high pressure, residual soil organic matters and the like on the inner wall of the stirring and mixing tank are removed, the cleaning of the device is guaranteed, the influence of the residual matters on the subsequent soil improvement work is avoided, the stable performance of the soil improvement operation is further guaranteed, meanwhile, the corrosion to parts of the device is reduced, the maintenance and replacement cost is reduced, and the service life of the device is prolonged.|DRAWINGS DESCRIPTION|[0014] FIG. 1 is a schematic perspective view of a soil carbon sequestration improvement apparatus according to the present utility model;|[0015] FIG. 2 is a schematic view of another angle structure of a soil carbon sequestration improvement apparatus according to the present utility model; |[0016] FIG. 3 is a schematic view showing the structure of an improved device for fixing carbon in soil according to the present utility model; |[0017] fig. 4 is a schematic view of a partial cross-sectional structure of a soil carbon sequestration improvement apparatus according to the present utility model. |[0018] The machine is characterized by comprising a stirring mixing tank 1, a tank cover 2, a feeding hole 3, a rotary motor 4, a rotary motor 5, a rotary shaft 6, a crushing cutter 7, a stirring motor 8, a transmission shaft 9, a stirring rod 10, a scraping plate 11, an auger 12, an organic fertilizer box 13, a conveying pipe 14, a valve 15, a watering rack 16, a flushing pipe 17, a connecting pipe 18, a pump 19, a water tank 20, a supporting frame 21 and a blanking pipe.|INVENTION MODE|Detailed Description|[0019] In order that the above objects, features and advantages of the utility model will be more clearly understood, a further description of the utility model will be rendered by reference to the appended drawings and examples. It should be noted that, without conflict, the embodiments of the present utility model and features in the embodiments may be combined with each other.|[0020] In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present utility model, but the present utility model may be practiced otherwise than as described herein, and therefore the present utility model is not limited to the specific embodiments of the disclosure that follow.|[0021] The embodiment 1 of the utility model is as shown in figures 1-4, the utility model provides a technical scheme, which comprises a stirring and mixing tank 1, a tank cover 2 is arranged at the top of the stirring and mixing tank 1, a feed inlet 3 is connected to the top of the tank cover 2, a rotating motor 4 is arranged on the side surface of the feed inlet 3, one end of the rotating motor 4 is connected with a rotating shaft 5, a plurality of crushing cutters 6 are distributed on the outer side of the rotating shaft 5, a stirring motor 7 is arranged at the top of the tank cover 2, a transmission shaft 8 is connected to the bottom of the stirring motor 7, a plurality of stirring rods 9 are distributed on the outer side of the transmission shaft 8, one end of the stirring rod 9 is connected with a scraping plate 10, a packing auger 11 is connected to the bottom of the transmission shaft 8, a blanking pipe 21 is connected to the bottom of the stirring and mixing tank 1, a conveying pipe 13 is connected to the top of the conveying pipe 13, an organic fertilizer box 12 is connected to the top of the conveying pipe 13, a valve 14 is arranged in the middle of the conveying pipe 13, a top of the organic fertilizer box 12 is connected to the bottom of the organic fertilizer box 12, and the bottom of a supporting block is connected to the bottom of the feeding pipe 2.|[0022] In this embodiment, the inside of pouring into stirring blending tank 1 with soil has been made things convenient for through feed inlet 3, before the inside of soil entering stirring blending tank 1, electric drive axis of rotation 5 rotates through rotating motor 4, and then make axis of rotation 5 drive broken sword 6 rotate, be favorable to realizing broken sword 6 break up the soil of caking, be favorable to increasing the hole of soil, make the soil structure become loose, then open valve 14, make the inside fertilizer of fertilizer case 12 carry to the inside of watering frame 15 through conveyer pipe 13 under the effect of gravity, spray out through the shower nozzle of watering frame 15 bottom at last, simultaneously rotate through stirring motor 7 electric drive transmission shaft 8, make stirring rod 9 stir soil and fertilizer, be favorable to making soil and fertilizer intensive mixing, the condition of fertilizer mixing inequality has been avoided, and then the solid carbon effect of soil has been increased, scraper blade 10 is favorable to scraping the remaining soil of stirring blending tank 1 inner wall, the homogeneity of soil and fertilizer mixing has been improved, after soil and fertilizer mixing is accomplished, make the effect of soil and fertilizer mix through conveyer pipe 13, the inside is favorable to carrying out the waste material through stirring rod 21 under the effect of stirring drum 1, the mixed soil is improved, the mixed material is favorable to the soil through stirring rod is carried out under the mixed material through stirring drum 11, the mixed material mixing drum is carried out under the soil is improved, the mixed effect is improved, the soil is improved through the mixed soil is carried out under the mixed material is better than the mixed soil is under the mixed material is well through stirring drum is under the mixed with the soil is under the condition of waste is well mixed through the soil is 11.|[0023] In embodiment 2, as shown in fig. 1-4, a flushing pipe 16 is arranged on the inner side of the stirring and mixing tank 1, a plurality of high-pressure nozzles are distributed at the bottom of the flushing pipe 16, a connecting pipe 17 is connected to the side surface of the flushing pipe 16, a pump 18 is connected to one end of the connecting pipe 17, a water tank 19 is arranged at the bottom of the pump 18, a supporting frame 20 is arranged on the outer side of the stirring and mixing tank 1, and the bottom of the water tank 19 is connected with the top of the supporting frame 20.|[0024] In this embodiment, after the improvement of soil solid carbon is accomplished, the inside water source of water tank 19 is taken out through pump 18, make the water source carry to the inside of wash pipe 16 through connecting pipe 17, last through the high-pressure nozzle blowout of wash pipe 16 bottom distribution, be favorable to effectively getting high-pressure washing to the inner wall of stirring blending tank 1, be favorable to cleaing away the remaining soil organic matter of stirring blending tank 1 inner wall etc. and be favorable to guaranteeing the cleanness of device, avoid remaining material to influence subsequent soil improvement work, and then guaranteed the stability of soil improvement operation and go on, reduce the corruption to device spare part simultaneously, maintenance and replacement cost have been reduced, the life of device has been prolonged.|[0025] The working principle of the embodiment is as follows: when using, at first feed inlet 3 has made things convenient for pouring soil into the inside of stirring blending tank 1, before soil gets into the inside of stirring blending tank 1, electric drive axis of rotation 5 rotates through rotating motor 4, and then make axis of rotation 5 drive broken sword 6 rotate, be favorable to realizing that broken sword 6 breaks up the soil of caking, then open valve 14, make the inside fertilizer of fertilizer case 12 carry to the inside of watering frame 15 through conveyer pipe 13 under the effect of gravity, finally spout through the shower nozzle of watering frame 15 bottom, simultaneously rotate through stirring motor 7 electric drive transmission shaft 8, make stirring rod 9 stir soil and fertilizer, scraper blade 10 is favorable to striking off the remaining soil of stirring blending tank 1 inner wall, the homogeneity of soil and fertilizer mixture has been improved, after soil and fertilizer mixture are accomplished, the inside through feed inlet 3 is added organic waste, again through stirring motor 7 drive stirring rod 9 rotation, make organic waste and soil mix evenly, be favorable to increasing the carbon content of soil, after soil mixture is accomplished, through the soil mixture pipe 21, the soil is gone out the improvement in-out through the conveyer pipe is carried out to the high-pressure water source 17, the inside is favorable to the water pump is accomplished to the soil, the inside is washed to the water source is carried out to the soil through the high-pressure 17, the inside is washed to the water source is accomplished through the conveyer pipe 17, the high-pressure is washed to the inside of soil is accomplished through the conveyer pipe 17, the inside is washed through the water pump 17, the inside is well-down, the inside is washed to be washed to the inside the soil is well to be well to the soil is well to be well down.|[0026] The present utility model is not limited to the above-mentioned embodiments, and any equivalent embodiments which can be changed or modified by the technical content disclosed above can be applied to other fields, but any simple modification, equivalent changes and modification made to the above-mentioned embodiments according to the technical substance of the present utility model without departing from the technical content of the present utility model still belong to the protection scope of the technical solution of the present utility model. (CN222852656)|TECHNICAL FIELD|Technical Field|[0001] The utility model relates to the technical field of soil carbon fixing devices, in particular to a soil carbon fixing improvement device.|BACKGROUND ART|[0002] Carbon sequestration in soil is one of means for reducing carbon emissions by combining carbon dioxide already present in the atmosphere and then converting it into a stable carbonaceous compound and storing it in the soil for a long period of time, and the organic carbon content and sequestration capacity in the soil are closely related to the fertility of the soil and crop yield, so that for poor soil with barren desertification, microbial reduction of the soil, and massive loss of organic carbon in the soil, carbon sequestration improvement by technical means is required to improve the carbon sequestration capacity of the soil.|[0003] In the prior art, in the stage of soil carbon fixation improvement, the soil and the organic fertilizer are required to be mixed, so that the organic carbon content in the soil is improved, but the existing soil is seriously agglomerated and is difficult to uniformly mix with the organic fertilizer, so that the soil carbon fixation effect is insufficient, and the problem of reduction of the soil improvement effect is caused.|DISCLOSURE|Disclosure of utility model|[0004] The utility model aims to solve the problems that in the prior art, soil is seriously agglomerated and is difficult to uniformly mix with an organic fertilizer, so that the soil carbon fixation effect is insufficient, and the soil improvement effect is reduced.|[0005] In order to achieve the purpose, the soil carbon fixation improvement device comprises a stirring and mixing tank, wherein a tank cover is arranged at the top of the stirring and mixing tank, a feed inlet is connected to the top of the tank cover, a rotating motor is arranged on the side face of the feed inlet, one end of the rotating motor is connected with a rotating shaft, a plurality of crushing cutters are distributed on the outer side of the rotating shaft, a stirring motor is arranged at the top of the tank cover, a transmission shaft is connected to the bottom of the stirring motor, and a plurality of stirring rods are distributed on the outer side of the transmission shaft.|[0006] Preferably, a flushing pipe is arranged on the inner side of the stirring and mixing tank, a plurality of high-pressure nozzles are distributed at the bottom of the flushing pipe, a connecting pipe is connected to the side face of the flushing pipe, a pump is connected to one end of the connecting pipe, and a water tank is arranged at the bottom of the pump.|[0007] Preferably, one end of the stirring rod is connected with a scraping plate, the bottom of the transmission shaft is connected with a packing auger, the bottom of the stirring and mixing tank is connected with a discharging pipe, and the outer side of the packing auger is connected with the inner wall of the discharging pipe.|[0008] Preferably, the internally mounted of stirring blending tank has the watering frame, the top of watering frame is connected with the conveyer pipe, the top of conveyer pipe is connected with the fertilizer case, the middle part of conveyer pipe is provided with the valve.|[0009] Preferably, the top of the organic fertilizer box is connected with a feeding pipe, a supporting block is arranged at the bottom of the organic fertilizer box, and the bottom of the supporting block is connected with the top of the tank cover.|[0010] Preferably, a supporting frame is arranged on the outer side of the stirring and mixing tank, and the bottom of the water tank is connected with the top of the supporting frame.|[0011] Compared with the prior art, the utility model has the advantages and positive effects that,|[0012] 1. According to the utility model, the rotating shaft is driven to rotate by the motor, so that the rotating shaft drives the crushing cutter to rotate, the crushing cutter is beneficial to scattering soil of a block, the pore space of the soil is increased, the soil structure is loosened, the soil and the organic fertilizer are fully and uniformly mixed, the condition of uneven mixing of the organic fertilizer is avoided, the soil quality is improved, and the soil carbon fixation effect is further improved.|[0013] 2. According to the utility model, the water source in the water tank is pumped by the pump, the water source is conveyed into the flushing pipe through the connecting pipe, and finally the water source is sprayed out through the high-pressure nozzles distributed at the bottom of the flushing pipe, so that the inner wall of the stirring and mixing tank is effectively flushed under high pressure, residual soil organic matters and the like on the inner wall of the stirring and mixing tank are removed, the cleaning of the device is guaranteed, the influence of the residual matters on the subsequent soil improvement work is avoided, the stable performance of the soil improvement operation is further guaranteed, meanwhile, the corrosion to parts of the device is reduced, the maintenance and replacement cost is reduced, and the service life of the device is prolonged.|DRAWINGS DESCRIPTION|[0014] FIG. 1 is a schematic perspective view of a soil carbon sequestration improvement apparatus according to the present utility model;|[0015] FIG. 2 is a schematic view of another angle structure of a soil carbon sequestration improvement apparatus according to the present utility model; |[0016] FIG. 3 is a schematic view showing the structure of an improved device for fixing carbon in soil according to the present utility model; |[0017] fig. 4 is a schematic view of a partial cross-sectional structure of a soil carbon sequestration improvement apparatus according to the present utility model. |[0018] The machine is characterized by comprising a stirring mixing tank 1, a tank cover 2, a feeding hole 3, a rotary motor 4, a rotary motor 5, a rotary shaft 6, a crushing cutter 7, a stirring motor 8, a transmission shaft 9, a stirring rod 10, a scraping plate 11, an auger 12, an organic fertilizer box 13, a conveying pipe 14, a valve 15, a watering rack 16, a flushing pipe 17, a connecting pipe 18, a pump 19, a water tank 20, a supporting frame 21 and a blanking pipe.|INVENTION MODE|Detailed Description|[0019] In order that the above objects, features and advantages of the utility model will be more clearly understood, a further description of the utility model will be rendered by reference to the appended drawings and examples. It should be noted that, without conflict, the embodiments of the present utility model and features in the embodiments may be combined with each other.|[0020] In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present utility model, but the present utility model may be practiced otherwise than as described herein, and therefore the present utility model is not limited to the specific embodiments of the disclosure that follow.|[0021] The embodiment 1 of the utility model is as shown in figures 1-4, the utility model provides a technical scheme, which comprises a stirring and mixing tank 1, a tank cover 2 is arranged at the top of the stirring and mixing tank 1, a feed inlet 3 is connected to the top of the tank cover 2, a rotating motor 4 is arranged on the side surface of the feed inlet 3, one end of the rotating motor 4 is connected with a rotating shaft 5, a plurality of crushing cutters 6 are distributed on the outer side of the rotating shaft 5, a stirring motor 7 is arranged at the top of the tank cover 2, a transmission shaft 8 is connected to the bottom of the stirring motor 7, a plurality of stirring rods 9 are distributed on the outer side of the transmission shaft 8, one end of the stirring rod 9 is connected with a scraping plate 10, a packing auger 11 is connected to the bottom of the transmission shaft 8, a blanking pipe 21 is connected to the bottom of the stirring and mixing tank 1, a conveying pipe 13 is connected to the top of the conveying pipe 13, an organic fertilizer box 12 is connected to the top of the conveying pipe 13, a valve 14 is arranged in the middle of the conveying pipe 13, a top of the organic fertilizer box 12 is connected to the bottom of the organic fertilizer box 12, and the bottom of a supporting block is connected to the bottom of the feeding pipe 2.|[0022] In this embodiment, the inside of pouring into stirring blending tank 1 with soil has been made things convenient for through feed inlet 3, before the inside of soil entering stirring blending tank 1, electric drive axis of rotation 5 rotates through rotating motor 4, and then make axis of rotation 5 drive broken sword 6 rotate, be favorable to realizing broken sword 6 break up the soil of caking, be favorable to increasing the hole of soil, make the soil structure become loose, then open valve 14, make the inside fertilizer of fertilizer case 12 carry to the inside of watering frame 15 through conveyer pipe 13 under the effect of gravity, spray out through the shower nozzle of watering frame 15 bottom at last, simultaneously rotate through stirring motor 7 electric drive transmission shaft 8, make stirring rod 9 stir soil and fertilizer, be favorable to making soil and fertilizer intensive mixing, the condition of fertilizer mixing inequality has been avoided, and then the solid carbon effect of soil has been increased, scraper blade 10 is favorable to scraping the remaining soil of stirring blending tank 1 inner wall, the homogeneity of soil and fertilizer mixing has been improved, after soil and fertilizer mixing is accomplished, make the effect of soil and fertilizer mix through conveyer pipe 13, the inside is favorable to carrying out the waste material through stirring rod 21 under the effect of stirring drum 1, the mixed soil is improved, the mixed material is favorable to the soil through stirring rod is carried out under the mixed material through stirring drum 11, the mixed material mixing drum is carried out under the soil is improved, the mixed effect is improved, the soil is improved through the mixed soil is carried out under the mixed material is better than the mixed soil is under the mixed material is well through stirring drum is under the mixed with the soil is under the condition of waste is well mixed through the soil is 11.|[0023] In embodiment 2, as shown in fig. 1-4, a flushing pipe 16 is arranged on the inner side of the stirring and mixing tank 1, a plurality of high-pressure nozzles are distributed at the bottom of the flushing pipe 16, a connecting pipe 17 is connected to the side surface of the flushing pipe 16, a pump 18 is connected to one end of the connecting pipe 17, a water tank 19 is arranged at the bottom of the pump 18, a supporting frame 20 is arranged on the outer side of the stirring and mixing tank 1, and the bottom of the water tank 19 is connected with the top of the supporting frame 20.|[0024] In this embodiment, after the improvement of soil solid carbon is accomplished, the inside water source of water tank 19 is taken out through pump 18, make the water source carry to the inside of wash pipe 16 through connecting pipe 17, last through the high-pressure nozzle blowout of wash pipe 16 bottom distribution, be favorable to effectively getting high-pressure washing to the inner wall of stirring blending tank 1, be favorable to cleaing away the remaining soil organic matter of stirring blending tank 1 inner wall etc. and be favorable to guaranteeing the cleanness of device, avoid remaining material to influence subsequent soil improvement work, and then guaranteed the stability of soil improvement operation and go on, reduce the corruption to device spare part simultaneously, maintenance and replacement cost have been reduced, the life of device has been prolonged.|[0025] The working principle of the embodiment is as follows: when using, at first feed inlet 3 has made things convenient for pouring soil into the inside of stirring blending tank 1, before soil gets into the inside of stirring blending tank 1, electric drive axis of rotation 5 rotates through rotating motor 4, and then make axis of rotation 5 drive broken sword 6 rotate, be favorable to realizing that broken sword 6 breaks up the soil of caking, then open valve 14, make the inside fertilizer of fertilizer case 12 carry to the inside of watering frame 15 through conveyer pipe 13 under the effect of gravity, finally spout through the shower nozzle of watering frame 15 bottom, simultaneously rotate through stirring motor 7 electric drive transmission shaft 8, make stirring rod 9 stir soil and fertilizer, scraper blade 10 is favorable to striking off the remaining soil of stirring blending tank 1 inner wall, the homogeneity of soil and fertilizer mixture has been improved, after soil and fertilizer mixture are accomplished, the inside through feed inlet 3 is added organic waste, again through stirring motor 7 drive stirring rod 9 rotation, make organic waste and soil mix evenly, be favorable to increasing the carbon content of soil, after soil mixture is accomplished, through the soil mixture pipe 21, the soil is gone out the improvement in-out through the conveyer pipe is carried out to the high-pressure water source 17, the inside is favorable to the water pump is accomplished to the soil, the inside is washed to the water source is carried out to the soil through the high-pressure 17, the inside is washed to the water source is accomplished through the conveyer pipe 17, the high-pressure is washed to the inside of soil is accomplished through the conveyer pipe 17, the inside is washed through the water pump 17, the inside is well-down, the inside is washed to be washed to the inside the soil is well to be well to the soil is well to be well down.|[0026] The present utility model is not limited to the above-mentioned embodiments, and any equivalent embodiments which can be changed or modified by the technical content disclosed above can be applied to other fields, but any simple modification, equivalent changes and modification made to the above-mentioned embodiments according to the technical substance of the present utility model without departing from the technical content of the present utility model still belong to the protection scope of the technical solution of the present utility model. Family Number|(114517722)|114517722|Abstract|(CN222852656U U)|The utility model provides an improved soil carbon sequestration device , which relates to the technical field of soil carbon sequestration devices and comprises a stirring and mixing tank , a tank cover is mounted at the top of the stirring and mixing tank , a feeding port is connected to the top of the tank cover , a rotating motor is mounted on the side face of the feeding port , one end of the rotating motor is connected with a rotating shaft , and the other end of the rotating shaft is connected with a rotating shaft . A plurality of crushing cutters are distributed on the outer side of the rotating shaft , a stirring motor is mounted at the top of the tank cover , a transmission shaft is connected to the bottom of the stirring motor , and a plurality of stirring sticks are distributed on the outer side of the transmission shaft . According to the device , the rotating shaft is electrically driven to rotate through the rotating motor , so that the rotating shaft drives the crushing cutters to rotate , the crushing cutters can scatter caked soil , soil pores can be increased , the soil structure becomes loose , the soil and an organic fertilizer can be fully and uniformly mixed , and the soil and the organic fertilizer can be uniformly mixed . The condition of non - uniform mixing of the organic fertilizer is avoided , the soil quality is improved , and the soil carbon sequestration effect is further improved . |IPC codes|(CN222852656U U)|A01B - 071/08 |A01B - 077/00 |A01C - 015/00 |A01C - 015/12 |B01F - 033/83 |B01F - 035/11 |B01F - 101/32 |Title|(CN222852656U U)|Soil carbon sequestration improvement device | Chemical engineering|Other special machines A01B-071/08|A01B-077/00|A01C-015/00|A01C-015/12|B01F-033/83|B01F-035/11|B01F-101/32 A01B-071/08|A01B-077/00|A01C-015/00|A01C-015/12|B01F-033/83|B01F-035/11|B01F-101/32 GRANTED (CN222852656)|GRANTED ALIVE (CN222852656)|ALIVE (CN222852656)|LEGAL DETAILS FOR CN222852656|Actual or expected expiration date=2034-07-29|Legal state=ALIVE|Status=GRANTED|Event publication date=2024-07-29|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202421798515|Application date=2024-07-29|Standardized application number=2024CN-U1798515|Event publication date=2025-05-13|Event code=CN/U|Event indicator=Pos|Event group=Event indicating In Force|Registered Utility Model|Publication country=CN|Publication number=CN222852656|Publication stage code=U|Publication date=2025-05-13|Standardized publication number=CN222852656U|Event publication date=2025-05-13|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN222852656)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=TIBu/CuuJksqylcw1H42TaqLeopS8oZMbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000077472095&ekey=2615&xpn=CN222852656U&kind=U https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=tc9rmHCTvYHqOrToLEA9bLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN222852656)|CN (CN222852656)|NAME=FUJIAN DUNFENG TANHUI AGRICULTURAL TECHNOLOGY CO., LTD. , COUNTRY=CN (CN222852656)|NAME=LIU YONGQING;BEIJING DAWSON ZHIGU INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) et al. , REG=33468 (CN222852656)|NAME=KANG QUAN|NAME=KANG XIAOXIONG 0 1 Titre: (CN222852656)|Soil carbon sequestration improvement device Résumé: (CN222852656)|The utility model provides an improved soil carbon sequestration device, which relates to the technical field of soil carbon sequestration devices and comprises a stirring and mixing tank, a tank cover is mounted at the top of the stirring and mixing tank, a feeding port is connected to the top of the tank cover, a rotating motor is mounted on the side face of the feeding port, one end of the rotating motor is connected with a rotating shaft, and the other end of the rotating shaft is connected with a rotating shaft. A plurality of crushing cutters are distributed on the outer side of the rotating shaft, a stirring motor is mounted at the top of the tank cover, a transmission shaft is connected to the bottom of the stirring motor, and a plurality of stirring sticks are distributed on the outer side of the transmission shaft. According to the device, the rotating shaft is electrically driven to rotate through the rotating motor, so that the rotating shaft drives the crushing cutters to rotate, the crushing cutters can scatter caked soil, soil pores can be increased, the soil structure becomes loose, the soil and an organic fertilizer can be fully and uniformly mixed, and the soil and the organic fertilizer can be uniformly mixed. The condition of non-uniform mixing of the organic fertilizer is avoided, the soil quality is improved, and the soil carbon sequestration effect is further improved. 41 Abstract gpt-4o-mini no The article focuses on a device for improving soil carbon sequestration through mixing and crushing, but does not mention accelerated weathering or mineral carbonation processes related to CO₂ capture.
42 CN202210827283 CN202210827283 CN115191303 102170837 CN115191303 A 2022-10-18 [CN115191303] 2022-07-14 2022-07-14 2022-10-18 (CN115191303)|2024-12-20 (CN115191303)|Emission reduction and carbon sequestration rice cultivation method for winter paddy field (CN115191303)|The invention discloses a winter paddy field emission reduction and carbon sequestration rice cultivation method which comprises the following steps: selecting a winter paddy field of which the soil bulk density is less than 1g/cm < 3 >, crushing straws and returning the straws to the field, and applying a fermented organic fertilizer, biomass charcoal and a chemical synthetic fertilizer; water-saving and fertilizer-saving rice variety seedlings are selected, and no-tillage cultivation is adopted; after the rice is cultivated, rainwater is collected for shallow water irrigation, after 35-45 days, drainage and field drying are conducted till the rice begins to be jointed, and then rainwater is collected for deep water irrigation till full heading is achieved; and 14-16 days after full heading, draining water and drying the field, and then harvesting the rice. Compared with a conventional rice cultivation technology, the method has the advantages that the total nitrogen leaching rate is reduced by 30% or above, the emission of N2O and CH4 is reduced by 30% or above, the carbon sequestration amount of soil in unit area in one year is increased by 29% or above, technical support is provided for improvement of winter paddy field cultivated land soil organic matter, emission reduction of agricultural greenhouse gas and sustainable development of agriculture, and the method is worthy of popularization and application. The method has great significance for ensuring the food safety and the sustainable development of agriculture in China. RICE CHINESE SORGHUM RESEARCH INSTITUTE SICHUAN ACADEMY OF AGRICULTURAL SCIENCES (CN115191303)|RICE CHINESE SORGHUM RESEARCH INSTITUTE SICHUAN ACADEMY OF AGRICULTURAL SCIENCES ([CN]) ZHANG LIN|LIU MAO|CHEN LIN|XU FUXIAN|JIANG PENG|GUO XIAOYI|ZHOU XINGBING|ZHU YONGCHUAN|XIONG HONG (CN115191303)|ZHANG LIN|LIU MAO|CHEN LIN|XU FUXIAN|JIANG PENG|GUO XIAOYI|ZHOU XINGBING|ZHU YONGCHUAN|XIONG HONG (CN115191303)|HE FAN;BEIJING ZHENGHUA ZHICHENG PATENT AGENCY|Reg. Nb: 11870 (CN115191303)|Improving the soil fertility: compared with the conventional rice cultivation technology, the method has the advantages that the straw is completely crushed and returned to the field, and the fermented organic fertilizer and the biomass charcoal are applied additionally, so that the physical and chemical properties of the soil are improved, and the soil fertility is improved.| (CN115191303)|1. A method for cultivating rice in winter paddy fields by reducing emission and fixing carbon is characterized by comprising the following steps:(1) Selecting soil with volume weight less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied;(2) Selecting water-saving and fertilizer-saving rice seedlings, and cultivating in a no-tillage mode;(3) After the rice is cultivated, rainwater is collected for irrigation, after 35-45 days, the water is drained and the field is sunned until the rice begins to be subjected to jointing, and then rainwater is collected for irrigation until the rice is flush with the ears;(4) Draining and drying the field 14-16 days after the ears are aligned, and then harvesting first season rice;(5) And (3) irrigating water and steeping the first season rice after harvesting, carrying out shallow water irrigation from seedling emergence to heading stage, wetting and irrigating until the first season rice is mature after heading, and harvesting ratoon rice.| (CN115191303)|In order to solve the technical problems, the invention aims to provide a method for cultivating the carbon-fixing and emission-reducing rice in the winter paddy field, so as to solve the problem that the existing carbon-fixing and emission-reducing rice cultivation method in the winter paddy field is poor in technical effect.|The invention discloses a method for cultivating carbon-fixing rice in winter paddy field with emission reduction, which comprises the following steps: selecting soil with volume weight less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied; selecting water-saving and fertilizer-saving rice seedlings, and cultivating in a no-tillage way; after the rice is cultivated, rainwater is collected for irrigation, after 35-45 days, the water is drained and the field is sunned until the rice begins to be subjected to jointing, and then rainwater is collected for irrigation until the rice is flush with the ears; and (5) after the ear is leveled for 14-16d, draining and drying the field, and then harvesting the rice.|The invention relates to the technical field of rice cultivation, in particular to a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon.| (CN115191303)|WINTER PADDY FIELD(100,42)|EMISSION REDUCTION(100,20)|RICE CULTIVATION(100,17)|CARBON FIXING RICE(100,12)|FIXING CARBON(100,5)|FERTILIZER SAVING RICE SEEDLING(100,4)|BIOMASS CHARCOAL(82,13)|SYNTHESIZED FERTILIZER(72,9)|SEASON RICE(70,29)|HARVESTING RATOON RICE(66,5)|RICE SEEDLING(64,5)|IRRIGATION(57,14)|FERMENTED ORGANIC FERTILIZER(54,13)|RICE(53,24)|RAINWATER(49,8)|SEEDLING EMERGENCE(47,3)|AGRICULTURE SUSTAINABLE DEVELOPMENT(44,4)|EAR(39,9)|PHOSPHATE FERTILIZER(37,12)|STRAW(34,9)|JOINT(29,6)|DRAINING(27,5)|EMISSION REDUCING RICE CULTIVATION(26,1)|EMISSION REDUCING RICE(24,1)|SOIL FERTILITY(23,6)|PADDY RICE CULTIVATION(23,4)|REDUCING EMISSION(21,3)|AGRICULTURAL GREENHOUSE GAS(21,2)|VOLUME WEIGHT(20,3)|GROUND(19,19)|SOIL CHEMICAL PROPERTY(18,2)|CULTIVATED LAND(18,1)|CULTIVATION LAYER THICKNESS(18,1)|NITROGENOUS FERTILIZER(17,6)|SIGNIFICANCE(17,2)|SOIL ORGANIC MATTER PROMOTION(17,1)|WATER SAVING(15,13)|CARBON FIXING(15,3)|NITROGEN LEACHING LOSS RATE(15,2)|WETTING(14,5)|FERMENTED ORGANIC FERTILIZER DOSAGE(14,4)|POTASH FERTILIZER(14,4)|POTASSIUM FERTILIZER(13,8)|THOUSAND HM(13,2)|HARVESTER(12,6)|RATOON RICE(12,3)|NITROGEN FERTILIZER(11,8)|SOIL CARBON CONTENT(11,3)|REGENERATED RICE EAR(11,1)|SEASON RICE YIELD(10,2)|EAR ALIGNING(9,3)|MUD(9,2)|FOOT(8,5)|NITROGEN UTILIZATION RATE(8,5)|CHEMICAL PROPERTY(8,2)|FARMLAND ECOSYSTEM(8,1)|ANNUAL UNIT AREA(7,3)|DEMONSTRATION VERIFICATION(7,1)|FERTILIZER CONSERVATION(7,1)|FUSHUN COUNTY(7,1)|LUXIAN COUNTY(7,1)|RATOONING RICE YIELD(7,1)|RICE LEISURE(7,1)|SYNTHETIC FERTILIZER(6,5)|ENSURING GRAIN SAFETY(6,1)|MOISTURE MANAGEMENT YIELD(6,1)|RELIEVING GLOBAL WARMING(6,1)|SEASON RICE GROWTH PERIOD(6,1)|SOIL HYDROLYZABLE NITROGEN CONTENT(6,1)|GUILLOTINE(5,2)|TECHNICAL SUPPORT(5,2)|ALKALI DIFFUSION(5,1)|CUTTER ROLLER(5,1)|DROUGHT TOLERANCE INDEX(5,1)|FERTILIZATION MODE INFLUENCE(5,1)|PADDY YIELD FORMATION(5,1)|PLOW LAYER SOIL(5,1)|RAIN COLLECTION(5,1)|REDUCING FARMLAND SOIL(5,1)|RICE AVERAGE YIELD(5,1)|ROTARY TILLAGE(5,1)|SOIL CARBON RESERVOIR RESERVE(5,1)|SOIL FERTILITY DETECTION(5,1)|CARBON FIXATION(4,5)|YIELD DIFFERENCE(4,5)|HEADING MENSTRUATION(4,2)|ROTARY CULTIVATOR(4,2)|AGRICULTURAL MANAGEMENT MEASURE(4,1)|AMMONIUM ACETATE LEACHING(4,1)|AMMONIUM NITROGEN CONTENT(4,1)|FARMLAND GREENHOUSE GAS EMISSION(4,1)|GREENHOUSE GAS METHANE(4,1)|IRRIGATION WATER(4,1)|ITEM SOIL VOLUME(4,1)|MAXIMUM SEEDLING(4,1)|MOISTURE TREATMENT(4,1)|NITRATE NITROGEN CONTENT(4,1)|PADDY PLANTING MECHANIZED OPERATION(4,1)|PLOW LAYER THICKNESS(4,1)|RICE YIELD FORMATION(4,1)|TOTAL FERTILIZER(4,1)|CARRYING OUT SHALLOW(3,3)|RAIN COLLECTING DEEP WATER(3,3)|STEM TILLER NUMBER(3,3)|AGE LIMIT(3,2)|AGRICULTURE(3,1)|ATMOSPHERE EMISSION SOURCE(3,1)| (CN115191303)|1. A method for cultivating rice in winter paddy fields by reducing emission and fixing carbon is characterized by comprising the following steps:|(1) Selecting soil with volume weight less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied;|(2) Selecting water-saving and fertilizer-saving rice seedlings, and cultivating in a no-tillage mode;|(3) After the rice is cultivated, rainwater is collected for irrigation, after 35-45 days, the water is drained and the field is sunned until the rice begins to be subjected to jointing, and then rainwater is collected for irrigation until the rice is flush with the ears;|(4) Draining and drying the field 14-16 days after the ears are aligned, and then harvesting first season rice;|(5) And (3) irrigating water and steeping the first season rice after harvesting, carrying out shallow water irrigation from seedling emergence to heading stage, wetting and irrigating until the first season rice is mature after heading, and harvesting ratoon rice.|2. The method for cultivating carbon-fixing rice in winter paddy with reduced emission according to claim 1, wherein the thickness of the cultivation layer in the step (1) is 5-30cm.|3. The method for cultivating carbon-fixing rice in winter paddy field as claimed in claim 1, wherein the amount of the organic fertilizer fermented in step (1) is 45-60kg/hm as calculated as pure N 2 。|4. The method for cultivating carbon-fixing rice in winter paddy field with emission reduction as claimed in claim 1, wherein the amount of biomass charcoal in step (1) is 8-12t/hm 2 。|5. The method for cultivating the carbon-fixing rice in the winter paddy field with emission reduction function according to claim 1, wherein the chemical synthesized fertilizer in the step (1) is a mixture of a nitrogenous fertilizer, a phosphate fertilizer and a potash fertilizer; wherein the dosage of the nitrogen fertilizer is 25-35kg/hm calculated by pure N 2 The amount of phosphate fertilizer is P 2 O 5 Measured in a range of 55-65kg/hm 2 The dosage of the potassium fertilizer is K 2 The O is 55-65kg/hm 2 。|6. The method for cultivating carbon-fixing rice in winter paddy fields with emission reduction according to claim 1, wherein the nitrogen utilization rate of the water-saving and fertilizer-saving rice variety in the step (2) is more than 50%.|7. The method for cultivating the carbon-fixing rice in the winter paddy field with reduced emission according to claim 1, wherein the drought tolerance index of the water-saving and fertilizer-saving rice variety in the step (2) is more than 0.9.|8. The method for cultivating the carbon-fixing rice in the winter paddy field with reduced emission according to claim 1, wherein the harvest index of the water-saving and fertilizer-saving rice variety in the step (2) is more than 0.56.|9. The method for cultivating carbon-fixing rice in winter paddy field with emission reduction according to claim 1Characterized in that the number of the whole-field stem tillers in the step (3) reaches 165-195 ten thousand/hm 2 And then the water is drained to dry the land.|10. The method for cultivating carbon-fixing rice in winter paddy field as claimed in claim 1, wherein the rice is not stuck with mud and falls into soil when being dried to be treaded by feet in the step (4). (CN115191303)|TECHNICAL FIELD|[0001] The invention relates to the technical field of rice cultivation, in particular to a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon.|BACKGROUND ART|[0002] The agricultural production process discharges a large amount of greenhouse gas methane (CH) 4 ) And nitrous oxide (N) 2 O), reducing farmland soil CH 4 And N 2 O emission and improvement of soil carbon reservoir reserves (carbon fixation and emission reduction for short) are important for relieving global warming and ensuring grain safety. The research of 23428shows that a farmland ecosystem not only has greenhouse gas emission but also has absorption, and is an active area for greenhouse gas exchange of a ground-gas interface, agriculture is an important emission source of atmospheric greenhouse gas, particularly the paddy field ecosystem is an important emission source of the atmosphere, the contribution of a paddy field to the greenhouse effect cannot be small, the greenhouse gas emission of a winter paddy field is paid much attention in various paddy fields, the winter paddy field is a common paddy field ecosystem in the south and the southwest areas of China, the particularity of the winter paddy field lies in that water storage and leisure of rice are carried out to transplanting the rice in the next year after the rice is harvested in autumn, the water covering time is long, the greenhouse gas emission flux is large, meanwhile, the greenhouse gas emission of farmlands such as the winter paddy fields is greatly influenced by agricultural management measures, such as water management, tillage, fertilization and the like can cause the physical and chemical environment change of soil, so that the activity of microorganisms is influenced, and the greenhouse gas emission can also change along with the greenhouse gas emission. Therefore, the purpose of changing the greenhouse gas emission mode can be achieved by changing the water and fertilizer management of the paddy field and other ways, however, the current paddy field carbon-fixing rice cultivation technology for reducing emission in winter has no good effect.|DISCLOSURE|Disclosure of Invention|[0003] In order to solve the technical problems, the invention aims to provide a method for cultivating the carbon-fixing and emission-reducing rice in the winter paddy field, so as to solve the problem that the existing carbon-fixing and emission-reducing rice cultivation method in the winter paddy field is poor in technical effect.|[0004] The technical scheme for solving the technical problems is as follows: the method for cultivating the carbon-fixing rice in the winter paddy field by emission reduction comprises the following steps:|[0005] (1) Selecting soil with volume weight less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied;|[0006] (2) Selecting water-saving and fertilizer-saving rice seedlings, and cultivating in a no-tillage mode;|[0007] (3) After the rice is cultivated, rainwater is collected for irrigation, after 35-45 days, the water is drained and the field is sunned until the rice begins to be subjected to jointing, and then rainwater is collected for irrigation until the rice is flush with the ears;|[0008] (4) Draining and drying the field 14-16 days after the ear aligning, and then harvesting first season rice;|[0009] (5) And (3) irrigating the first season rice after harvesting, soaking the first season rice in the field, sprouting the first season rice until the heading period is short-water irrigated, wetting and irrigating the first season rice until the first season rice is mature after heading, and harvesting ratoon rice.|[0010] The beneficial effects of the invention are as follows: compared with the conventional rice cultivation technology, the total nitrogen leaching loss rate is reduced by more than 30 percent, and N is 2 O and CH 4 The emission reduction is more than 30%, the annual unit area soil carbon content is increased by more than 29%, technical support is provided for soil organic matter improvement of winter paddy fields, emission reduction of agricultural greenhouse gases and sustainable development of agriculture, and great significance is brought to grain safety and sustainable development of agriculture in China.|[0011] On the basis of the technical scheme, the invention can be further improved as follows:|[0012] further, the thickness of the intertillage layer in the step (1) is 5-30cm.|[0013] Further, the dosage of the fermented organic fertilizer in the step (1) is 45-60kg/hm calculated by pure N 2 。|[0014] Further, the amount of the biomass charcoal in the step (1) is 8-12t/hm 2 。|[0015] Further, the chemical synthesized fertilizer in the step (1) is a mixture of a nitrogenous fertilizer, a phosphate fertilizer and a potash fertilizer; wherein the dosage of the nitrogen fertilizer is 25-35kg/hm calculated by pure N 2 The amount of phosphate fertilizer is P 2 O 5 Measured as 55-65kg/hm 2 The amount of the potassium fertilizer is K 2 The O is 55-65kg/hm 2 。|[0016] Further, the nitrogen utilization rate of the water-saving and fertilizer-saving rice variety in the step (2) is more than 50 percent.|[0017] Further, the drought tolerance index of the water-saving and fertilizer-saving rice variety in the step (2) is more than 0.9.|[0018] Further, the harvest index of the water-saving and fertilizer-saving rice variety in the step (2) is more than 0.56.|[0019] Further, the number of the tillering seedlings in the whole field in the step (3) reaches 165-195 ten thousand/hm 2 And then the water is drained to dry the land.|[0020] And (5) further, drying the field in the sun until the field is treaded by feet, so that mud is not trapped and is not stuck.|[0021] The invention has the following beneficial effects:|[0022] 1. water and fertilizer conservation: compared with the current large-area popularization of rice cultivation technology, the method reduces the total fertilizer amount and can reduce N90kg/hm through water-saving fertilizer-saving variety breeding and high-efficiency water management technology 2 、P 2 O 5 90kg/hm 2 And K 2 O 90kg/hm 2 And simultaneously greatly reduces the amount of irrigation water.|[0023] 2. High yield and synergism: compared with the conventional rice cultivation technology, the invention can increase the yield of rice by 900kg/hm averagely 2 The yield is increased by more than 10%, and the mechanized operation of paddy planting in winter paddy fields can be realized by means of field sunning, so that high yield and efficiency improvement are realized.|[0024] 3. Improving the soil fertility: compared with the conventional rice cultivation technology, the method has the advantages that the straw is completely crushed and returned to the field, and the fermented organic fertilizer and the biomass charcoal are applied additionally, so that the physical and chemical properties of the soil are improved, and the soil fertility is improved.|DRAWINGS DESCRIPTION|[0025] FIG. 1 is a graph showing the linear correlation between the yield difference between plowed and no-tillage rice and the no-tillage year.|INVENTION MODE|Detailed Description|[0026] The principles and features of this invention are described below in conjunction with the following drawings, which are set forth to illustrate, but are not to be construed to limit the scope of the invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.|[0027] Example 1:|[0028] a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon comprises the following steps:|[0029] (1) The thickness of the selected plough layer is 8cm, and the volume weight of the soil is less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied; wherein the dosage of the fermented organic fertilizer is 50kg/hm in terms of pure N 2 (ii) a The using amount of the biomass charcoal is 10t/hm 2 The chemical synthetic fertilizer is a mixture of a nitrogenous fertilizer, a phosphate fertilizer and a potash fertilizer, and the dosage of the nitrogenous fertilizer is 30kg/hm by pure N 2 The amount of the phosphate fertilizer is P 2 O 5 Measured as 60kg/hm 2 The dosage of the potassium fertilizer is K 2 O is 60kg/hm 2 ;|[0030] (2) Selecting water-saving and fertilizer-saving rice variety seedlings with nitrogen utilization rate of more than 50%, drought resistance index of more than 0.9 and harvest index of more than 0.56, and cultivating in a no-tillage mode;|[0031] (3) The rice is irrigated in shallow water after being cultivated, and the number of stem tillers in the whole field reaches 180 ten thousand per hm after 40 days 2 When the rice field is drained, the field is dried till the rice begins to be subjected to jointing, and then the field is irrigated in rain-collecting deep water till the rice is flush with ears;|[0032] (4) Draining and drying the field 15d after the ear aligning until the field is not sunk and stuck by feet, and then harvesting first season rice;|[0033] (5) And (3) irrigating water and steeping the first season rice after harvesting, carrying out shallow water irrigation from seedling emergence to heading stage, wetting and irrigating until the first season rice is mature after heading, and harvesting ratoon rice.|[0034] Example 2:|[0035] a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon comprises the following steps:|[0036] (1) Selecting a plough layer with the thickness of 30cm and the soil volume weight of less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied; wherein the dosage of the fermented organic fertilizer is 60kg/hm calculated by pure N 2 (ii) a The biomass charcoal dosage is 12t/hm 2 The chemical synthetic fertilizer is a mixture of a nitrogenous fertilizer, a phosphate fertilizer and a potash fertilizer, and the dosage of the nitrogenous fertilizer is 35kg/hm by pure N 2 The amount of the phosphate fertilizer is P 2 O 5 Measured as 65kg/hm 2 The amount of the potassium fertilizer is K 2 The O content is 65kg/hm 2 ;|[0037] (2) Selecting water-saving and fertilizer-saving rice seedlings with nitrogen utilization rate more than 50%, drought tolerance index more than 0.9 and harvest index more than 0.56, and cultivating in a no-tillage mode;|[0038] (3) After rice cultivation, rainwater is collected for irrigation, and after 45 days, the number of stem tillers in the whole field reaches 195 ten thousand per hm 2 When the rice field is drained, the field is dried till the rice begins to be subjected to jointing, and then the field is irrigated in rain-collecting deep water till the rice is flush with ears;|[0039] (4) Draining and drying the field 16d after the ear aligning until the field is not sunk and stuck by feet, and then harvesting first season rice;|[0040] (5) And (3) irrigating water and steeping the first season rice after harvesting, carrying out shallow water irrigation from seedling emergence to heading stage, wetting and irrigating until the first season rice is mature after heading, and harvesting ratoon rice.|[0041] Example 3:|[0042] a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon comprises the following steps:|[0043] (1) Selecting a plough layer with the thickness of 5cm and the soil volume weight of less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied; wherein the dosage of the fermented organic fertilizer is 45kg/hm in terms of pure N 2 (ii) a The using amount of the biomass charcoal is 8t/hm 2 The chemical synthetic fertilizer is a mixture of a nitrogen fertilizer, a phosphate fertilizer and a potassium fertilizer, and the dosage of the nitrogen fertilizer is 25kg/hm in terms of pure N 2 The amount of phosphate fertilizer is P 2 O 5 Measured as 55kg/hm 2 The amount of the potassium fertilizer is K 2 The O is 55kg/hm 2 ;|[0044] (2) Selecting water-saving and fertilizer-saving rice variety seedlings with nitrogen utilization rate of more than 50%, drought resistance index of more than 0.9 and harvest index of more than 0.56, and cultivating in a no-tillage mode;|[0045] (3) After rice cultivation, rainwater is collected for irrigation, and after 35d, the number of stem tillers in the whole field reaches 165 ten thousand per hm 2 When the rice field is drained, the field is dried till the rice begins to be subjected to jointing, and then the field is irrigated in rain-collecting deep water till the rice is flush with ears;|[0046] (4) Draining water and drying the field until the soil is not sunk and stuck when the soil is treaded by feet 14d after the heading is finished, and then harvesting first season rice;|[0047] (5) And (3) irrigating the first season rice after harvesting, soaking the first season rice in the field, sprouting the first season rice until the heading period is short-water irrigated, wetting and irrigating the first season rice until the first season rice is mature after heading, and harvesting ratoon rice.|[0048] Comparative example 1:|[0049] a method for cultivating paddy rice in winter paddy fields comprises the following steps:|[0050] cultivation was carried out by plowing, and the rest was the same as in example 1.|[0051] Comparative example 2:|[0052] a method for cultivating paddy rice in winter paddy field comprises the following steps:|[0053] straw is not returned to the field, fermented organic fertilizer and biomass charcoal are not applied, and only chemical synthetic fertilizer is applied, wherein the application amount of the nitrogen fertilizer is 180kg/hm calculated by pure N 2 The amount of the phosphate fertilizer is P 2 O 5 The meter is 150kg/hm 2 K is the amount of potassium fertilizer applied 2 O is 150kg/hm 2 Otherwise, the same procedure as in example 1 was repeated.|[0054] Comparative example 3:|[0055] a method for cultivating paddy rice in winter paddy field comprises the following steps:|[0056] the first season rice is maintained in a certain water layer in the whole growth period, the first season rice is harvested, water is not filled into the field for soaking, rain is collected and irrigated until the ratoon rice is mature, and the rest is the same as the example 1.|[0057] Comparative example 4:|[0058] a method for cultivating paddy rice in winter paddy fields comprises the following steps:|[0059] (1) Selecting a plough layer with the thickness of 8cm and the soil volume weight of less than 1g/cm 3 Applying a chemical synthetic fertilizer to the winter paddy field; wherein the application amount of the nitrogen fertilizer is 180kg/hm calculated by pure N 2 The amount of the phosphate fertilizer is P 2 O 5 The meter is 150kg/hm 2 K is the amount of potassium fertilizer applied 2 O is 150kg/hm 2 ;|[0060] (2) Selecting common rice seedlings, and cultivating in a turning mode;|[0061] (3) Maintaining a certain water layer in the whole growth period of the first season rice, and then harvesting the first season rice;|[0062] (4) Harvesting the first season rice, collecting rain and irrigating until the ratoon rice is mature, and harvesting the ratoon rice.|[0063] Test examples|[0064] 1. Changes in physical properties and fertility of soil|[0065] The physical properties and the fertility change of the soil in the winter paddy field after long-term cultivation in the embodiment 1 and the comparative example 1 are detected, and the specific detection method of the soil physical properties comprises the following steps: the bulk density of the soil was determined by the guillotine method, and the porosity of the soil was determined by the guillotine method, and the results are shown in table 1. The specific detection method of the soil fertility comprises the following steps: the content of organic carbon in the soil is measured by a potassium dichromate volumetric method-external heating method, the content of total nitrogen in the soil is measured by a Kjeldahl method, the content of total phosphorus in the soil is measured by an alkali fusion method, the content of total potassium in the soil is measured by an alkali fusion method, the content of hydrolyzable nitrogen in the soil is measured by an alkali diffusion method, the content of available phosphorus in the soil is measured by a colorimetric method, the content of quick-acting potassium in the soil is measured by an ammonium acetate leaching method, the content of nitrate nitrogen in the soil is measured by a phenoldisulfonic acid colorimetric method, and the content of ammonium nitrogen in the soil is measured by an indophenol blue colorimetric method, and the results are shown in Table 2.|[0066] TABLE 1 physical Properties of soil|[0067] ItemSoil volume weight mg/cm 3Porosity%Example 1109.558.89Comparative example 176.6272.18|[0068] TABLE 2 soil fertility|[0069] |[0070] As can be seen from the table 1-2, after continuous no-tillage, the volume weight of the 8cm plough layer soil is improved by 42.9%, the porosity is reduced by 18.4%, compared with the tillage, the no-tillage obviously improves the content of soil hydrolyzable nitrogen and organic carbon, and the no-tillage has an obvious carbon fixation effect.|[0071] 2. Long term no-tillage rice yield variation|[0072] The rice yields of the winter paddy fields after long-term cultivation in example 1 and comparative example 1 are counted, the yield difference value and the age limit of the comparative example 1 and example 1 are plotted, and the result is shown in fig. 1 (NT and CT respectively indicate no-tillage and no-tillage), as can be seen from fig. 1, the yield difference of the no-tillage rice and the no-tillage rice is in linear positive correlation with the age limit, the longer the no-tillage age is, the larger the yield difference of the no-tillage rice and the no-tillage is, therefore, the no-tillage age limit is an important factor influencing the yield difference of the no-tillage rice, the long-term no-tillage is not beneficial to the formation of the rice yield, but the no-tillage has obvious carbon fixation effect, therefore, when the volume weight of the winter soil of the paddy fields is less than 1g/cm 3 The rice field adopts no-tillage cultivation; the volume weight of the soil is more than 1g/cm 3 The rotary cultivator for the paddy field adopts the rotary cultivator with the maximum rotary radius of the cutter roller being less than 245mm and the water ploughing depth being less than 18cm to carry out rotary tillage, thus not only playing the carbon fixation function of no tillage, but also being beneficial to the formation of paddy yield, and meeting the requirement of mechanized operation on the unit weight of the plough layer of the paddy field.|[0073] 3. Influence of different fertilization modes on rice yield|[0074] The rice yields after cultivation in example 1 and comparative example 2 were counted and the results are shown in Table 3. As can be seen from Table 3, the total amount of straws is smashed and returned to the field in winter paddy fields, the fermented organic fertilizer and the biomass charcoal are applied additionally to improve the physical and chemical properties of the soil and improve the fertility of the soil, and the chemical synthesized fertilizer is deeply applied mechanically to realize the reduction of the application of nitrogen fertilizer in winter paddy fields and obviously improve the yield level of rice, so that the yield of rice can be obviously improved by the fertilizing method provided by the invention.|[0075] TABLE 3 Rice yields|[0076] |[0077] 4. Effect of different Water management on Rice yield|[0078] The yields of first season rice and regenerated rice after cultivation in example 1 and comparative example 3 were counted, and the results are shown in tables 4 to 5.|[0079] TABLE 4 first season rice yield|[0080] |[0081] TABLE 5 ratooning rice yield|[0082] |[0083] As can be seen from tables 4-5, the difference between the first season rice yield and the ear grain structure reaches an extremely significant level in different moisture treatments, and the yield of the moisture management method is significantly higher than that of the conventional method, mainly because the moisture management method of the invention significantly increases the maximum seedling and effective ear number of the first season rice and increases the effective ear of the regenerated rice, the rice yield can be significantly increased by the cultivation method of the invention.|[0084] 5. Yield of different rice varieties|[0085] The rice variety of example 1 was changed to a different rice variety, and the rice was cultivated according to the cultivation method of example 1, and the total yield was counted, and the results are shown in Table 6.|[0086] TABLE 6 yield of different rice varieties|[0087] |[0088] |[0089] As can be seen from Table 6, the varieties having high drought tolerance index, nitrogen fertilizer recycling rate and harvest index of the present invention can achieve high yield.|[0090] 6. Demonstration verification|[0091] According to the cultivation methods of the example 1 and the comparative example 4, the typical winter paddy field such as Luxian county, fushun county and the like in Sichuan province in 2018-2021The area demonstrates the method and the results are shown in table 7. As can be seen from Table 7, compared with the conventional cultivation technology of rice, the carbon fixation and emission reduction rice cultivation method for winter paddy field reduces the total nitrogen leaching loss rate by more than 30.0 percent, and N is 2 O and CH 4 The emission reduction is more than 30.0 percent, the annual unit area soil carbon content is increased by more than 29 percent, and the N is reduced by 90kg/hm 2 、P 2 O 5 90kg/hm 2 、K 2 O 90kg/hm 2 And the average yield of the rice is increased by 900kg/hm 2 Above, the yield is increased by more than 10%.|[0092] TABLE 7 comparison of the effects of the method of the present invention and conventional techniques|[0093] |[0094] |[0095] The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein. (CN115191303)|TECHNICAL FIELD|[0001] The invention relates to the technical field of rice cultivation, in particular to a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon.|BACKGROUND ART|[0002] The agricultural production process discharges a large amount of greenhouse gas methane (CH) 4 ) And nitrous oxide (N) 2 O), reducing farmland soil CH 4 And N 2 O emission and improvement of soil carbon reservoir reserves (carbon fixation and emission reduction for short) are important for relieving global warming and ensuring grain safety. The research of 23428shows that a farmland ecosystem not only has greenhouse gas emission but also has absorption, and is an active area for greenhouse gas exchange of a ground-gas interface, agriculture is an important emission source of atmospheric greenhouse gas, particularly the paddy field ecosystem is an important emission source of the atmosphere, the contribution of a paddy field to the greenhouse effect cannot be small, the greenhouse gas emission of a winter paddy field is paid much attention in various paddy fields, the winter paddy field is a common paddy field ecosystem in the south and the southwest areas of China, the particularity of the winter paddy field lies in that water storage and leisure of rice are carried out to transplanting the rice in the next year after the rice is harvested in autumn, the water covering time is long, the greenhouse gas emission flux is large, meanwhile, the greenhouse gas emission of farmlands such as the winter paddy fields is greatly influenced by agricultural management measures, such as water management, tillage, fertilization and the like can cause the physical and chemical environment change of soil, so that the activity of microorganisms is influenced, and the greenhouse gas emission can also change along with the greenhouse gas emission. Therefore, the purpose of changing the greenhouse gas emission mode can be achieved by changing the water and fertilizer management of the paddy field and other ways, however, the current paddy field carbon-fixing rice cultivation technology for reducing emission in winter has no good effect.|DISCLOSURE|Disclosure of Invention|[0003] In order to solve the technical problems, the invention aims to provide a method for cultivating the carbon-fixing and emission-reducing rice in the winter paddy field, so as to solve the problem that the existing carbon-fixing and emission-reducing rice cultivation method in the winter paddy field is poor in technical effect.|[0004] The technical scheme for solving the technical problems is as follows: the method for cultivating the carbon-fixing rice in the winter paddy field by emission reduction comprises the following steps:|[0005] (1) Selecting soil with volume weight less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied;|[0006] (2) Selecting water-saving and fertilizer-saving rice seedlings, and cultivating in a no-tillage mode;|[0007] (3) After the rice is cultivated, rainwater is collected for irrigation, after 35-45 days, the water is drained and the field is sunned until the rice begins to be subjected to jointing, and then rainwater is collected for irrigation until the rice is flush with the ears;|[0008] (4) Draining and drying the field 14-16 days after the ear aligning, and then harvesting first season rice;|[0009] (5) And (3) irrigating the first season rice after harvesting, soaking the first season rice in the field, sprouting the first season rice until the heading period is short-water irrigated, wetting and irrigating the first season rice until the first season rice is mature after heading, and harvesting ratoon rice.|[0010] The beneficial effects of the invention are as follows: compared with the conventional rice cultivation technology, the total nitrogen leaching loss rate is reduced by more than 30 percent, and N is 2 O and CH 4 The emission reduction is more than 30%, the annual unit area soil carbon content is increased by more than 29%, technical support is provided for soil organic matter improvement of winter paddy fields, emission reduction of agricultural greenhouse gases and sustainable development of agriculture, and great significance is brought to grain safety and sustainable development of agriculture in China.|[0011] On the basis of the technical scheme, the invention can be further improved as follows:|[0012] further, the thickness of the intertillage layer in the step (1) is 5-30cm.|[0013] Further, the dosage of the fermented organic fertilizer in the step (1) is 45-60kg/hm calculated by pure N 2 。|[0014] Further, the amount of the biomass charcoal in the step (1) is 8-12t/hm 2 。|[0015] Further, the chemical synthesized fertilizer in the step (1) is a mixture of a nitrogenous fertilizer, a phosphate fertilizer and a potash fertilizer; wherein the dosage of the nitrogen fertilizer is 25-35kg/hm calculated by pure N 2 The amount of phosphate fertilizer is P 2 O 5 Measured as 55-65kg/hm 2 The amount of the potassium fertilizer is K 2 The O is 55-65kg/hm 2 。|[0016] Further, the nitrogen utilization rate of the water-saving and fertilizer-saving rice variety in the step (2) is more than 50 percent.|[0017] Further, the drought tolerance index of the water-saving and fertilizer-saving rice variety in the step (2) is more than 0.9.|[0018] Further, the harvest index of the water-saving and fertilizer-saving rice variety in the step (2) is more than 0.56.|[0019] Further, the number of the tillering seedlings in the whole field in the step (3) reaches 165-195 ten thousand/hm 2 And then the water is drained to dry the land.|[0020] And (5) further, drying the field in the sun until the field is treaded by feet, so that mud is not trapped and is not stuck.|[0021] The invention has the following beneficial effects:|[0022] 1. water and fertilizer conservation: compared with the current large-area popularization of rice cultivation technology, the method reduces the total fertilizer amount and can reduce N90kg/hm through water-saving fertilizer-saving variety breeding and high-efficiency water management technology 2 、P 2 O 5 90kg/hm 2 And K 2 O 90kg/hm 2 And simultaneously greatly reduces the amount of irrigation water.|[0023] 2. High yield and synergism: compared with the conventional rice cultivation technology, the invention can increase the yield of rice by 900kg/hm averagely 2 The yield is increased by more than 10%, and the mechanized operation of paddy planting in winter paddy fields can be realized by means of field sunning, so that high yield and efficiency improvement are realized.|[0024] 3. Improving the soil fertility: compared with the conventional rice cultivation technology, the method has the advantages that the straw is completely crushed and returned to the field, and the fermented organic fertilizer and the biomass charcoal are applied additionally, so that the physical and chemical properties of the soil are improved, and the soil fertility is improved.|DRAWINGS DESCRIPTION|[0025] FIG. 1 is a graph showing the linear correlation between the yield difference between plowed and no-tillage rice and the no-tillage year.|INVENTION MODE|Detailed Description|[0026] The principles and features of this invention are described below in conjunction with the following drawings, which are set forth to illustrate, but are not to be construed to limit the scope of the invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.|[0027] Example 1:|[0028] a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon comprises the following steps:|[0029] (1) The thickness of the selected plough layer is 8cm, and the volume weight of the soil is less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied; wherein the dosage of the fermented organic fertilizer is 50kg/hm in terms of pure N 2 (ii) a The using amount of the biomass charcoal is 10t/hm 2 The chemical synthetic fertilizer is a mixture of a nitrogenous fertilizer, a phosphate fertilizer and a potash fertilizer, and the dosage of the nitrogenous fertilizer is 30kg/hm by pure N 2 The amount of the phosphate fertilizer is P 2 O 5 Measured as 60kg/hm 2 The dosage of the potassium fertilizer is K 2 O is 60kg/hm 2 ;|[0030] (2) Selecting water-saving and fertilizer-saving rice variety seedlings with nitrogen utilization rate of more than 50%, drought resistance index of more than 0.9 and harvest index of more than 0.56, and cultivating in a no-tillage mode;|[0031] (3) The rice is irrigated in shallow water after being cultivated, and the number of stem tillers in the whole field reaches 180 ten thousand per hm after 40 days 2 When the rice field is drained, the field is dried till the rice begins to be subjected to jointing, and then the field is irrigated in rain-collecting deep water till the rice is flush with ears;|[0032] (4) Draining and drying the field 15d after the ear aligning until the field is not sunk and stuck by feet, and then harvesting first season rice;|[0033] (5) And (3) irrigating water and steeping the first season rice after harvesting, carrying out shallow water irrigation from seedling emergence to heading stage, wetting and irrigating until the first season rice is mature after heading, and harvesting ratoon rice.|[0034] Example 2:|[0035] a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon comprises the following steps:|[0036] (1) Selecting a plough layer with the thickness of 30cm and the soil volume weight of less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied; wherein the dosage of the fermented organic fertilizer is 60kg/hm calculated by pure N 2 (ii) a The biomass charcoal dosage is 12t/hm 2 The chemical synthetic fertilizer is a mixture of a nitrogenous fertilizer, a phosphate fertilizer and a potash fertilizer, and the dosage of the nitrogenous fertilizer is 35kg/hm by pure N 2 The amount of the phosphate fertilizer is P 2 O 5 Measured as 65kg/hm 2 The amount of the potassium fertilizer is K 2 The O content is 65kg/hm 2 ;|[0037] (2) Selecting water-saving and fertilizer-saving rice seedlings with nitrogen utilization rate more than 50%, drought tolerance index more than 0.9 and harvest index more than 0.56, and cultivating in a no-tillage mode;|[0038] (3) After rice cultivation, rainwater is collected for irrigation, and after 45 days, the number of stem tillers in the whole field reaches 195 ten thousand per hm 2 When the rice field is drained, the field is dried till the rice begins to be subjected to jointing, and then the field is irrigated in rain-collecting deep water till the rice is flush with ears;|[0039] (4) Draining and drying the field 16d after the ear aligning until the field is not sunk and stuck by feet, and then harvesting first season rice;|[0040] (5) And (3) irrigating water and steeping the first season rice after harvesting, carrying out shallow water irrigation from seedling emergence to heading stage, wetting and irrigating until the first season rice is mature after heading, and harvesting ratoon rice.|[0041] Example 3:|[0042] a method for cultivating rice in winter paddy fields by reducing emission and fixing carbon comprises the following steps:|[0043] (1) Selecting a plough layer with the thickness of 5cm and the soil volume weight of less than 1g/cm 3 In the winter paddy field, the straws are crushed and returned to the field, and a fermented organic fertilizer, biomass charcoal and a chemically synthesized fertilizer are applied; wherein the dosage of the fermented organic fertilizer is 45kg/hm in terms of pure N 2 (ii) a The using amount of the biomass charcoal is 8t/hm 2 The chemical synthetic fertilizer is a mixture of a nitrogen fertilizer, a phosphate fertilizer and a potassium fertilizer, and the dosage of the nitrogen fertilizer is 25kg/hm in terms of pure N 2 The amount of phosphate fertilizer is P 2 O 5 Measured as 55kg/hm 2 The amount of the potassium fertilizer is K 2 The O is 55kg/hm 2 ;|[0044] (2) Selecting water-saving and fertilizer-saving rice variety seedlings with nitrogen utilization rate of more than 50%, drought resistance index of more than 0.9 and harvest index of more than 0.56, and cultivating in a no-tillage mode;|[0045] (3) After rice cultivation, rainwater is collected for irrigation, and after 35d, the number of stem tillers in the whole field reaches 165 ten thousand per hm 2 When the rice field is drained, the field is dried till the rice begins to be subjected to jointing, and then the field is irrigated in rain-collecting deep water till the rice is flush with ears;|[0046] (4) Draining water and drying the field until the soil is not sunk and stuck when the soil is treaded by feet 14d after the heading is finished, and then harvesting first season rice;|[0047] (5) And (3) irrigating the first season rice after harvesting, soaking the first season rice in the field, sprouting the first season rice until the heading period is short-water irrigated, wetting and irrigating the first season rice until the first season rice is mature after heading, and harvesting ratoon rice.|[0048] Comparative example 1:|[0049] a method for cultivating paddy rice in winter paddy fields comprises the following steps:|[0050] cultivation was carried out by plowing, and the rest was the same as in example 1.|[0051] Comparative example 2:|[0052] a method for cultivating paddy rice in winter paddy field comprises the following steps:|[0053] straw is not returned to the field, fermented organic fertilizer and biomass charcoal are not applied, and only chemical synthetic fertilizer is applied, wherein the application amount of the nitrogen fertilizer is 180kg/hm calculated by pure N 2 The amount of the phosphate fertilizer is P 2 O 5 The meter is 150kg/hm 2 K is the amount of potassium fertilizer applied 2 O is 150kg/hm 2 Otherwise, the same procedure as in example 1 was repeated.|[0054] Comparative example 3:|[0055] a method for cultivating paddy rice in winter paddy field comprises the following steps:|[0056] the first season rice is maintained in a certain water layer in the whole growth period, the first season rice is harvested, water is not filled into the field for soaking, rain is collected and irrigated until the ratoon rice is mature, and the rest is the same as the example 1.|[0057] Comparative example 4:|[0058] a method for cultivating paddy rice in winter paddy fields comprises the following steps:|[0059] (1) Selecting a plough layer with the thickness of 8cm and the soil volume weight of less than 1g/cm 3 Applying a chemical synthetic fertilizer to the winter paddy field; wherein the application amount of the nitrogen fertilizer is 180kg/hm calculated by pure N 2 The amount of the phosphate fertilizer is P 2 O 5 The meter is 150kg/hm 2 K is the amount of potassium fertilizer applied 2 O is 150kg/hm 2 ;|[0060] (2) Selecting common rice seedlings, and cultivating in a turning mode;|[0061] (3) Maintaining a certain water layer in the whole growth period of the first season rice, and then harvesting the first season rice;|[0062] (4) Harvesting the first season rice, collecting rain and irrigating until the ratoon rice is mature, and harvesting the ratoon rice.|[0063] Test examples|[0064] 1. Changes in physical properties and fertility of soil|[0065] The physical properties and the fertility change of the soil in the winter paddy field after long-term cultivation in the embodiment 1 and the comparative example 1 are detected, and the specific detection method of the soil physical properties comprises the following steps: the bulk density of the soil was determined by the guillotine method, and the porosity of the soil was determined by the guillotine method, and the results are shown in table 1. The specific detection method of the soil fertility comprises the following steps: the content of organic carbon in the soil is measured by a potassium dichromate volumetric method-external heating method, the content of total nitrogen in the soil is measured by a Kjeldahl method, the content of total phosphorus in the soil is measured by an alkali fusion method, the content of total potassium in the soil is measured by an alkali fusion method, the content of hydrolyzable nitrogen in the soil is measured by an alkali diffusion method, the content of available phosphorus in the soil is measured by a colorimetric method, the content of quick-acting potassium in the soil is measured by an ammonium acetate leaching method, the content of nitrate nitrogen in the soil is measured by a phenoldisulfonic acid colorimetric method, and the content of ammonium nitrogen in the soil is measured by an indophenol blue colorimetric method, and the results are shown in Table 2.|[0066] TABLE 1 physical Properties of soil|[0067] ItemSoil volume weight mg/cm 3Porosity%Example 1109.558.89Comparative example 176.6272.18|[0068] TABLE 2 soil fertility|[0069] |[0070] As can be seen from the table 1-2, after continuous no-tillage, the volume weight of the 8cm plough layer soil is improved by 42.9%, the porosity is reduced by 18.4%, compared with the tillage, the no-tillage obviously improves the content of soil hydrolyzable nitrogen and organic carbon, and the no-tillage has an obvious carbon fixation effect.|[0071] 2. Long term no-tillage rice yield variation|[0072] The rice yields of the winter paddy fields after long-term cultivation in example 1 and comparative example 1 are counted, the yield difference value and the age limit of the comparative example 1 and example 1 are plotted, and the result is shown in fig. 1 (NT and CT respectively indicate no-tillage and no-tillage), as can be seen from fig. 1, the yield difference of the no-tillage rice and the no-tillage rice is in linear positive correlation with the age limit, the longer the no-tillage age is, the larger the yield difference of the no-tillage rice and the no-tillage is, therefore, the no-tillage age limit is an important factor influencing the yield difference of the no-tillage rice, the long-term no-tillage is not beneficial to the formation of the rice yield, but the no-tillage has obvious carbon fixation effect, therefore, when the volume weight of the winter soil of the paddy fields is less than 1g/cm 3 The rice field adopts no-tillage cultivation; the volume weight of the soil is more than 1g/cm 3 The rotary cultivator for the paddy field adopts the rotary cultivator with the maximum rotary radius of the cutter roller being less than 245mm and the water ploughing depth being less than 18cm to carry out rotary tillage, thus not only playing the carbon fixation function of no tillage, but also being beneficial to the formation of paddy yield, and meeting the requirement of mechanized operation on the unit weight of the plough layer of the paddy field.|[0073] 3. Influence of different fertilization modes on rice yield|[0074] The rice yields after cultivation in example 1 and comparative example 2 were counted and the results are shown in Table 3. As can be seen from Table 3, the total amount of straws is smashed and returned to the field in winter paddy fields, the fermented organic fertilizer and the biomass charcoal are applied additionally to improve the physical and chemical properties of the soil and improve the fertility of the soil, and the chemical synthesized fertilizer is deeply applied mechanically to realize the reduction of the application of nitrogen fertilizer in winter paddy fields and obviously improve the yield level of rice, so that the yield of rice can be obviously improved by the fertilizing method provided by the invention.|[0075] TABLE 3 Rice yields|[0076] |[0077] 4. Effect of different Water management on Rice yield|[0078] The yields of first season rice and regenerated rice after cultivation in example 1 and comparative example 3 were counted, and the results are shown in tables 4 to 5.|[0079] TABLE 4 first season rice yield|[0080] |[0081] TABLE 5 ratooning rice yield|[0082] |[0083] As can be seen from tables 4-5, the difference between the first season rice yield and the ear grain structure reaches an extremely significant level in different moisture treatments, and the yield of the moisture management method is significantly higher than that of the conventional method, mainly because the moisture management method of the invention significantly increases the maximum seedling and effective ear number of the first season rice and increases the effective ear of the regenerated rice, the rice yield can be significantly increased by the cultivation method of the invention.|[0084] 5. Yield of different rice varieties|[0085] The rice variety of example 1 was changed to a different rice variety, and the rice was cultivated according to the cultivation method of example 1, and the total yield was counted, and the results are shown in Table 6.|[0086] TABLE 6 yield of different rice varieties|[0087] |[0088] |[0089] As can be seen from Table 6, the varieties having high drought tolerance index, nitrogen fertilizer recycling rate and harvest index of the present invention can achieve high yield.|[0090] 6. Demonstration verification|[0091] According to the cultivation methods of the example 1 and the comparative example 4, the typical winter paddy field such as Luxian county, fushun county and the like in Sichuan province in 2018-2021The area demonstrates the method and the results are shown in table 7. As can be seen from Table 7, compared with the conventional cultivation technology of rice, the carbon fixation and emission reduction rice cultivation method for winter paddy field reduces the total nitrogen leaching loss rate by more than 30.0 percent, and N is 2 O and CH 4 The emission reduction is more than 30.0 percent, the annual unit area soil carbon content is increased by more than 29 percent, and the N is reduced by 90kg/hm 2 、P 2 O 5 90kg/hm 2 、K 2 O 90kg/hm 2 And the average yield of the rice is increased by 900kg/hm 2 Above, the yield is increased by more than 10%.|[0092] TABLE 7 comparison of the effects of the method of the present invention and conventional techniques|[0093] |[0094] |[0095] The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein. Family Number|(102170837)|102170837|Abstract|(CN115191303 A)|The invention discloses a winter paddy field emission reduction and carbon sequestration rice cultivation method which comprises the following steps : selecting a winter paddy field of which the soil bulk density is less than 1 g / cm < 3 > , crushing straws and returning the straws to the field , and applying a fermented organic fertilizer , biomass charcoal and a chemical synthetic fertilizer ; water - saving and fertilizer - saving rice variety seedlings are selected , and no - tillage cultivation is adopted ; after the rice is cultivated , rainwater is collected for shallow water irrigation , after 35-45 days , drainage and field drying are conducted till the rice begins to be jointed , and then rainwater is collected for deep water irrigation till full heading is achieved ; and 14-16 days after full heading , draining water and drying the field , and then harvesting the rice . Compared with a conventional rice cultivation technology , the method has the advantages that the total nitrogen leaching rate is reduced by 30% or above , the emission of N2O and CH4 is reduced by 30% or above , the carbon sequestration amount of soil in unit area in one year is increased by 29% or above , technical support is provided for improvement of winter paddy field cultivated land soil organic matter , emission reduction of agricultural greenhouse gas and sustainable development of agriculture , and the method is worthy of popularization and application . The method has great significance for ensuring the food safety and the sustainable development of agriculture in China . |CPC codes|(CN115191303 A)|A01C - 021/00/5 |A01G - 022/22 |IPC codes|(CN115191303 A)|A01C - 021/00 |A01G - 022/22 |Title|(CN115191303 A)|Emission reduction and carbon sequestration rice cultivation method for winter paddy field | Other special machines A01C-021/00/5|A01G-022/22 A01C-021/00/5|A01G-022/22 A01C-021/00|A01G-022/22 A01C-021/00|A01G-022/22 CN116114449 CN116114449 104949244 WHO=Examiner SELF=N CAT=A CN114287302|CN112166981|CN111587751|AU2020100519|CN110881373|CN110583401|CN110476752|CN110140616|CN108738454|CN106495893|CN106233857|CN107396788|CN105794351|CN101743871 CN114287302 99514297 WHO=Examiner SELF=N CAT=A|CN112166981 92172768 WHO=Examiner SELF=N CAT=A|CN111587751 90415283 WHO=Examiner SELF=Y CAT=A|AU2020100519 89004524 WHO=Examiner SELF=N CAT=A|CN110881373 87894931 WHO=Examiner SELF=N CAT=A|CN110583401 87030247 WHO=Examiner SELF=N CAT=A|CN110476752 86713924 WHO=Examiner SELF=N CAT=A|CN110140616 85747078 WHO=Examiner SELF=N CAT=A|CN108738454 81844883 WHO=Examiner SELF=N CAT=A|CN106495893 75651357 WHO=Examiner SELF=N CAT=A|CN106233857 74948830 WHO=Examiner SELF=N CAT=A|CN107396788 77887768 WHO=Examiner SELF=N CAT=A|CN105794351 73701266 WHO=Examiner SELF=N CAT=A|CN101743871 6971405 WHO=Examiner SELF=N CAT=A 周胜;宋祥甫;颜晓元;: &quot;水稻低碳生产研究进展&quot;, 中国水稻科学, vol. 27, no. 02, pages 213 - 222 (Cat. Y)|熊继东;: &quot;低碳农业技术――水稻再生栽培&quot;, 作物研究, no. 04, pages 341 - 344 (Cat. A)|王礼兵等: &quot;江西省旱优73再生稻示范表现及高产栽培技术&quot;, 园艺与种苗, vol. 42, no. 05, pages 76 - 77 (Cat. Y) CN101743871; CN105794351; CN106233857; CN106495893; CN107396788; CN108738454; CN110140616; CN110476752; CN110583401; CN110881373; AU2020100519; CN111587751; CN112166981; CN114287302 REVOKED (CN115191303)|REVOKED DEAD (CN115191303)|DEAD (CN115191303)|LEGAL DETAILS FOR CN115191303|Actual or expected expiration date=2024-12-20|Legal state=DEAD|Status=REVOKED|Event publication date=2022-07-14|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210827283|Application date=2022-07-14|Standardized application number=2022CN-0827283|Event publication date=2022-10-18|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115191303|Publication stage code=A|Publication date=2022-10-18|Standardized publication number=CN115191303|Event publication date=2022-10-18|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-11-04|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-12-20|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQ7kY+0mcXjKFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000065002252&ekey=2118&xpn=CN115191303&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=fAx4dvTt7P7AyoiUbreoApNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN115191303)|CN (CN115191303)|NAME=RICE CHINESE SORGHUM RESEARCH INSTITUTE SICHUAN ACADEMY OF AGRICULTURAL SCIENCES , COUNTRY=CN (CN115191303)|NAME=HE FAN;BEIJING ZHENGHUA ZHICHENG PATENT AGENCY , REG=11870 (CN115191303)|CN (CN115191303)|NAME=ZHANG LIN, COUNTRY=CN |NAME=LIU MAO|NAME=CHEN LIN|NAME=XU FUXIAN|NAME=JIANG PENG|NAME=GUO XIAOYI|NAME=ZHOU XINGBING|NAME=ZHU YONGCHUAN|NAME=XIONG HONG 0 1 Titre: (CN115191303)|Emission reduction and carbon sequestration rice cultivation method for winter paddy field Résumé: (CN115191303)|The invention discloses a winter paddy field emission reduction and carbon sequestration rice cultivation method which comprises the following steps: selecting a winter paddy field of which the soil bulk density is less than 1g/cm < 3 >, crushing straws and returning the straws to the field, and applying a fermented organic fertilizer, biomass charcoal and a chemical synthetic fertilizer; water-saving and fertilizer-saving rice variety seedlings are selected, and no-tillage cultivation is adopted; after the rice is cultivated, rainwater is collected for shallow water irrigation, after 35-45 days, drainage and field drying are conducted till the rice begins to be jointed, and then rainwater is collected for deep water irrigation till full heading is achieved; and 14-16 days after full heading, draining water and drying the field, and then harvesting the rice. Compared with a conventional rice cultivation technology, the method has the advantages that the total nitrogen leaching rate is reduced by 30% or above, the emission of N2O and CH4 is reduced by 30% or above, the carbon sequestration amount of soil in unit area in one year is increased by 29% or above, technical support is provided for improvement of winter paddy field cultivated land soil organic matter, emission reduction of agricultural greenhouse gas and sustainable development of agriculture, and the method is worthy of popularization and application. The method has great significance for ensuring the food safety and the sustainable development of agriculture in China. 42 Abstract gpt-4o-mini no The article focuses on rice cultivation methods and agricultural practices for emission reduction and carbon sequestration, but does not address accelerated weathering of minerals or CO₂ capture through mineral carbonation.
43 CN202511396551 CN202511396551 CN121241723 117291810 CN121241723 A 2026-01-02 [CN121241723] 2025-09-28 2025-09-28 2026-01-02 (CN121241723)|2045-09-28 (CN121241723)|Innovative application method for realizing carbon sequestration and emission reduction of straws in acid soil (CN121241723)|The invention discloses an innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil, which comprises the following steps: step 1, straw pretreatment: cleaning, drying and crushing the straw to obtain straw powder; 2, straw modification for carbon preparation, wherein straw powder and a magnesium salt solution are mixed, and magnesium modified biochar is prepared through a low-speed pyrolysis method; step 3, lime neutralization: lime is applied to the soil; step 4, mixing and deep burying: mixing the magnesium modified biochar and unmodified straw powder, injecting the mixture into the deep layer of the underground soil, and covering the unmodified straw powder in the step 1 on the surface layer of the soil; 5, later regulation and control, wherein a magnesium salt solution is supplemented in a drip irrigation mode; lime is applied to the soil to neutralize the soil, in the middle stage, the magnesium modified biochar prepared through straw pyrolysis is matched with straw powder to be applied to the deep layer and the surface of the soil respectively, in the later stage, a magnesium salt solution is supplemented through drip irrigation, the effective magnesium content of the soil is maintained for a long time, and short-term, middle-term and long-term continuous carbon sequestration and emission reduction are achieved. GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES INSTITUTE OF AGRICULTURAL RESOURCES & ENVIRONMENT (CN121241723)|GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES, INSTITUTE OF AGRICULTURAL RESOURCES AND ENVIRONMENT ([CN]) HUANG QIAOYI|TANG SHUANHU|HUANG XU|HUANG JIANFENG|WU TENGFEI|ZHANG MU|YI QIONG|PANG YUWAN|DING WUHAN|CENG KE|WU YONGPEI|LI PING|FU HONGTING|LUO HAIBIN (CN121241723)|HUANG QIAOYI|TANG SHUANHU|HUANG XU|HUANG JIANFENG|WU TENGFEI|ZHANG MU|YI QIONG|PANG YUWAN|DING WUHAN|CENG KE|WU YONGPEI|LI PING|FU HONGTING|LUO HAIBIN (CN121241723)|WANG YONGZE;BEIJING SHENGGUANGXINHE IP FIRM|Reg. Nb: 16117 (CN121241723)|However, in the method for improving the utilization rate of the microbial carbon in the acid soil by using the lime in the straw returning field, under the traditional returning field mode, the decomposition rate of the straw is higher, the loss of active organic carbon is easy to cause, and the long-term carbon fixing effect cannot be ensured.|The invention has the beneficial effects that lime is applied to soil to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, so that the problem of acidizing the soil in a short period is solved, the advantage of quick neutralization effect of lime is fully utilized, the magnesium modified biochar prepared by crushing and soaking the straw in the magnesium salt solution in the middle period is respectively applied to the deep soil layer and the surface of the soil by matching with straw powder after pyrolysis, the acidity of the deep soil is neutralized for a long time in the middle period, the magnesium salt solution is supplemented by drip irrigation in the later period, the effective magnesium content of the soil is maintained for a long time, meanwhile, the formation of agglomerates is promoted while the earthworms are added to loosen the soil, the problem that carbon fixation and emission reduction can be realized in the acid soil continuously in the short period, the middle period and the long period is solved, and the problem that the single application of lime cannot take effect for a long time and secondary acidizing is easy is solved.| (CN121241723)|1. An innovative application method for realizing carbon fixation and emission reduction of straws in acid soil comprises the following steps: Firstly, preprocessing straws, namely cleaning and drying the straws, crushing the straws to the particle size of 0.1-0.3 mm, and filtering the crushed straws by a 20-mesh nylon screen to obtain uniform straw powder; step two, preparing charcoal by modifying straw, namely mixing the straw powder obtained in the step one with a magnesium salt solution at a rotating speed of 500-800 rpm, and preparing magnesium modified biochar by using a slow pyrolysis method; Thirdly, lime neutralization, lime is applied to the soil, and the lime application amount is 2-4 tons/hectare; Step four, mixing and deep burying, namely mixing the magnesium modified biochar prepared in the step two with the unmodified straw powder in the step one, injecting the mixture into the deep soil layer of 20-30 cm underground, and covering the unmodified straw powder in the step one on the surface layer of the soil; And fifthly, later-stage regulation and control, supplementing magnesium salt solution into the soil by adopting a drip irrigation mode, and synchronously adding earthworms into the soil. | (CN121241723)|Aiming at the problems, the invention aims to provide an innovative application method for realizing carbon fixation and emission reduction of straws in acid soil, which realizes the short-term alleviation of the problem of acidified soil by applying lime on the soil to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, fully utilizes the advantage of quick effect of lime neutralization, and adopts the method that magnesium modified biochar prepared by crushing and soaking the straws in a magnesium salt solution in the middle stage is respectively applied on the deep soil layer and the surface of the soil to realize the long-term neutralization of the deep soil acidity, adopts drip irrigation to supplement the magnesium salt solution in the later stage to realize the long-term maintenance of the effective magnesium content of the soil, and simultaneously promotes the formation of agglomerates when being matched with the addition of earthworms to loosen the soil, thereby realizing the long-term carbon fixation and emission reduction in the acid soil continuously in the short-term, middle-term and long-term, and effectively solving the problems that the single application of lime cannot realize long-term effect and secondary acidification is easy to cause.The invention aims at realizing the purposes by adopting the following technical scheme that the innovative application method for realizing carbon fixation and emission reduction of the straw in the acid soil comprises the following steps:|The invention discloses an innovative application method of straw in acid soil for realizing carbon fixation and emission reduction, which comprises the following steps of firstly, straw pretreatment, cleaning, drying and crushing the straw to obtain straw powder, secondly, straw modification charcoal preparation, mixing the straw powder with a magnesium salt solution, preparing magnesium modified biochar by a slow pyrolysis method, thirdly, lime neutralization, applying lime into soil, fourthly, mixing the magnesium modified biochar with the unmodified straw powder, deep-layer injection into the soil after mixing, and covering the soil surface layer with the unmodified straw powder in the first step, fifth, later regulation and control, and supplementing the magnesium salt solution by adopting a drip irrigation mode.|The invention relates to the technical field of agricultural ecology, in particular to an innovative application method for realizing carbon fixation and emission reduction of straws in acid soil.| (CN121241723)|EMISSION REDUCTION(100,18)|REALIZING CARBON FIXATION(100,10)|STRAW EMISSION REDUCTION(100,10)|UNMODIFIED STRAW POWDER(100,10)|ACIDIC SOIL(100,1)|LIME NEUTRALIZATION(64,8)|STRAW PRETREATMENT(59,1)|SLOW PYROLYSIS(52,9)|STRAW(51,35)|GROUND(50,33)|STRAW POWDER(49,13)|AGRICULTURAL ECOLOGY(49,1)|SOIL MAGNESIUM CONTENT(47,3)|LATE REGULATION(47,1)|GROUND LAYER DEPTH(45,4)|EXCHANGEABLE ALUMINUM ION(42,4)|STRAW MODIFICATION(42,1)|PREPROCESSING STRAW(39,4)|IMMEDIATE NEUTRALIZATION(38,1)|LIME(37,19)|CRUSHED STRAW(36,4)|MAGNESIUM SALT SOLUTION(35,30)|MAGNESIUM CONTENT(34,3)|BURYING DEPTH(33,2)|DRIP IRRIGATION MODE(32,6)|ACID SOIL(31,20)|MIDDLE PERIOD(31,3)|APPLYING LIME(30,4)|MODIFYING STRAW(29,4)|HYDROGEN ION NEUTRALIZATION(27,4)|UNIFORM STRAW POWDER(27,4)|ACIDIZING(27,1)|DRIP IRRIGATION(25,8)|ADDING EARTHWORM(24,4)|SOIL DEPTH(21,8)|MICROBIAL CARBON(21,3)|ACIDIFICATION(21,2)|DECOMPOSITION(21,1)|LATE PERIOD(21,1)|SOIL ACIDIFICATION(20,8)|UNDERGROUND(20,2)|TON HECTARE(19,8)|CRUSHING(19,6)|DEEP SOIL ACIDITY(19,3)|CARBON FIXATION(19,2)|CARBONIZATION REACTION(18,4)|LATE STAGE REGULATION(18,4)|DEEP LAYER INJECTION(18,1)|EARTHWORM(15,6)|SHORT TERM ALLEVIATION(15,1)|PYROLYSIS(14,7)|SHORT PERIOD(12,4)|BIOCHAR POROUS FRAMEWORK(12,2)|EARTHWORM ADDITION(12,2)|ROTATING SPEED(11,4)|ACTIVE ORGANIC CARBON(11,1)|LONG TERM NEUTRALIZATION(11,1)|MAGNESIUM ION(10,9)|MICROORGANISM POLLUTANT(10,2)|SOIL MICROENVIRONMENT(10,2)|STRAW BIOCHAR YIELD(10,2)|CARBON FIXING(10,1)|RISING TEMPERATURE(9,4)|LONG PERIOD(9,1)|LONG TERM MAINTENANCE(9,1)|MIDDLE TERM(9,1)|STEP FOUR(9,1)|STRAW MASS RATIO(8,4)|CELLULOSE DEEP CRACKING(8,2)|PRETREATED STRAW(8,2)|FIELD MODE RETURN(8,1)|RESTORATION PERIOD(8,1)|OXYGEN LIMITED SLOW PYROLYSIS(7,4)|BIOCHAR PORE(7,2)|IMPURITY INTERFERENCE(7,2)|SOIL ACIDIFICATION TOXICITY(7,2)|UTILIZATION RATE(7,2)|LONG TERM CARBON FIXATION(7,1)|ADSORB HYDROXYL(6,2)|LOADING UNIFORMITY(6,2)|OXYGEN LIMITING PYROLYSIS(6,2)|REDUCING MICROBIAL DECOMPOSITION(6,2)|SOIL AGGREGATE FORMATION(6,2)|ECOLOGICAL TASK(6,1)|IMPREGNATED STRAW(6,1)|SHORT TERM(6,1)|UNMODIFIED STRAW(6,1)|INORGANIC PHASE(5,4)|PARTICLE SIZE(5,4)|TUBE FURNACE(5,4)|IMPREGNATION(5,2)|MODIFIED BIOCHAR QUALITY STABILITY(5,2)|UNIFORM GRANULARITY(5,2)|COARSE FODDER(5,1)|CROP PHOTOSYNTHESIS PRODUCT(5,1)|FERTILIZER RETENTION CAPACITY(5,1)|FIELD MODE(5,1)|LONG TERM CARBON FIXING(5,1)|MATURE CROP(5,1)|MICROBIAL CARBON UTILIZATION(5,1)|MICROORGANISM ACTIVATION(5,1)|OYSTER SHELL(5,1)|RENEWABLE BIOLOGICAL RESOURCE(5,1)|STRAW CARBONIZED PRODUCT(5,1)|UNDERGROUND SOIL(5,1)|STRAW SURFACE(4,5)|SURFACE LAYER(4,5)|REPAIRING PERIOD(4,3)|CARBON RESERVOIR(4,2)|AGRICULTURE CARBON SEQUESTRATION CAPACITY(4,1)|AIR PERMEATION ISOLATION(4,1)|COARSE FIBER CONTENT(4,1)|MAGNESIUM MODIFIED BIOCHAR(4,1)|RESOURCE EFFICIENT CONVERSION(4,1)|SOIL CARBON SEQUESTRATION CAPACITY(4,1)|WHEAT REMAINDER(4,1)|ECONOMIC FEASIBILITY(3,2)|HEMICELLULOSE(3,2)|INSUFFICIENT REACTION(3,2)|LEACHING(3,2)| (CN121241723)|1. An innovative application method for realizing carbon fixation and emission reduction of straws in acid soil comprises the following steps:| Firstly, preprocessing straws, namely cleaning and drying the straws, crushing the straws to the particle size of 0.1-0.3 mm, and filtering the crushed straws by a 20-mesh nylon screen to obtain uniform straw powder; | step two, preparing charcoal by modifying straw, namely mixing the straw powder obtained in the step one with a magnesium salt solution at a rotating speed of 500-800 rpm, and preparing magnesium modified biochar by using a slow pyrolysis method; | Thirdly, lime neutralization, lime is applied to the soil, and the lime application amount is 2-4 tons/hectare; | Step four, mixing and deep burying, namely mixing the magnesium modified biochar prepared in the step two with the unmodified straw powder in the step one, injecting the mixture into the deep soil layer of 20-30 cm underground, and covering the unmodified straw powder in the step one on the surface layer of the soil; | And fifthly, later-stage regulation and control, supplementing magnesium salt solution into the soil by adopting a drip irrigation mode, and synchronously adding earthworms into the soil. |2. The innovative application method of the straw in the acid soil for realizing carbon fixation and emission reduction is characterized in that the concentration of the magnesium salt solution in the second step is 0.05-0.9 mol/L, and the mass ratio of straw powder to the solution is 1:5-1:20.|3. The innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil according to claim 1 is characterized in that the slow pyrolysis method in the second step is to heat to 500 ℃ in a tube furnace at a temperature rising speed of 5 ℃ per minute for oxygen-limited slow pyrolysis, and the carbonization reaction is completed after heat preservation for 1-3 hours.|4. The innovative application method for realizing carbon fixation and emission reduction of straw in acid soil according to claim 1 is characterized in that in the fourth step, the mass ratio of magnesium modified biochar to straw powder is 1:3, and the application amount is 5-8 tons/hectare.|5. The innovative application method of the straw in the acid soil for realizing carbon fixation and emission reduction is characterized in that the concentration of the magnesium salt solution for drip irrigation in the fifth step is 0.3-0.7 mol/L, and 1-2L/m 2 is supplemented once.|6. The innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil according to claim 1 is characterized in that the earthworm put-in density in the fifth step is 500-800 earthworms/m < 2 >, and the restoration period is 15-20 days. (CN121241723)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of agricultural ecology, in particular to an innovative application method for realizing carbon fixation and emission reduction of straws in acid soil.|BACKGROUND ART|[0002] Soil is the most important carbon reservoir of the land ecological system, the carbon reservoir amount is about 3 times of the atmosphere, soil carbon sequestration is recognized as the most potential, lowest cost and most easy to operate and realize technical approach, the reduction of carbon emission in the atmosphere and the reduction of greenhouse gas emission are one of important ecological tasks for coping with global climate change, while the agriculture and forestry ecological system plays an important role in carbon sequestration and emission reduction, the carbon sequestration capacity of the agriculture and forestry ecological system is enhanced mainly by increasing the organic carbon reserves and reducing the decomposition of organic carbon, the global carbon emission can be slowed down to a certain extent, and the acid soil carbon sequestration and emission reduction is a technical system for improving the carbon sequestration capacity of the soil and reducing the greenhouse gas emission through physical-chemical-biological synergism. The core is to utilize biochar (such as straw carbonized products) and mineral materials (such as oyster shells and wollastonite) to improve the acidity of soil.|[0003] The invention patent with the application number 202311059727.2 discloses a method for improving the utilization rate of microbial carbon in acid soil by applying lime to straw returning fields, which comprises the steps of firstly applying lime to soil, on one hand, fully neutralizing hydrogen ions in the soil by the lime, increasing the pH of the soil, on the other hand, activating microorganisms and eliminating external interference as much as possible, and then crushing the straw and returning the crushed straw to fields. The straw returning and lime applying method can obviously improve the utilization efficiency of the microbial carbon in the acid soil;|[0004] However, in the method for improving the utilization rate of the microbial carbon in the acid soil by using the lime in the straw returning field, under the traditional returning field mode, the decomposition rate of the straw is higher, the loss of active organic carbon is easy to cause, and the long-term carbon fixing effect cannot be ensured. |DISCLOSURE|Disclosure of Invention|[0005] Aiming at the problems, the invention aims to provide an innovative application method for realizing carbon fixation and emission reduction of straws in acid soil, which realizes the short-term alleviation of the problem of acidified soil by applying lime on the soil to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, fully utilizes the advantage of quick effect of lime neutralization, and adopts the method that magnesium modified biochar prepared by crushing and soaking the straws in a magnesium salt solution in the middle stage is respectively applied on the deep soil layer and the surface of the soil to realize the long-term neutralization of the deep soil acidity, adopts drip irrigation to supplement the magnesium salt solution in the later stage to realize the long-term maintenance of the effective magnesium content of the soil, and simultaneously promotes the formation of agglomerates when being matched with the addition of earthworms to loosen the soil, thereby realizing the long-term carbon fixation and emission reduction in the acid soil continuously in the short-term, middle-term and long-term, and effectively solving the problems that the single application of lime cannot realize long-term effect and secondary acidification is easy to cause.|[0006] The invention aims at realizing the purposes by adopting the following technical scheme that the innovative application method for realizing carbon fixation and emission reduction of the straw in the acid soil comprises the following steps:|[0007] Firstly, preprocessing straws, namely cleaning and drying the straws, crushing the straws to the particle size of 0.1-0.3 mm, and filtering the crushed straws by a 20-mesh nylon screen to obtain uniform straw powder; |[0008] step two, preparing charcoal by modifying straw, namely mixing the straw powder obtained in the step one with a magnesium salt solution at a rotating speed of 500-800 rpm, and preparing magnesium modified biochar by using a slow pyrolysis method; |[0009] Thirdly, lime neutralization, lime is applied to the soil, and the lime application amount is 2-4 tons/hectare; |[0010] Step four, mixing and deep burying, namely mixing the magnesium modified biochar prepared in the step two with the unmodified straw powder in the step one, injecting the mixture into the deep soil layer of 20-30 cm underground, and covering the unmodified straw powder in the step one on the surface layer of the soil; |[0011] And fifthly, later-stage regulation and control, supplementing magnesium salt solution into the soil by adopting a drip irrigation mode, and synchronously adding earthworms into the soil. |[0012] The further improvement is that the concentration of the magnesium salt solution in the second step is 0.05-0.9 mol/L, and the mass ratio of the straw powder to the solution is 1:5-1:20.|[0013] The further improvement is that the slow pyrolysis method in the second step is to heat to 500 ℃ in a tube furnace at a temperature rising speed of 5 ℃ per minute for oxygen-limited slow pyrolysis, and the carbonization reaction is completed after heat preservation for 1-3 hours.|[0014] The method is further improved in that in the fourth step, the mass ratio of the magnesium modified biochar to the straw powder is 1:3, and the application amount is 5-8 tons/hectare.|[0015] The further improvement is that the concentration of the magnesium salt solution for drip irrigation in the fifth step is 0.3-0.7 mol/L, and 1-2L/m < 2 > is supplemented once.|[0016] The method is further improved in that the earthworm putting density in the fifth step is 500-800 strips/m < 2 >, and the repairing period is 15-20 days.|[0017] The invention has the beneficial effects that lime is applied to soil to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, so that the problem of acidizing the soil in a short period is solved, the advantage of quick neutralization effect of lime is fully utilized, the magnesium modified biochar prepared by crushing and soaking the straw in the magnesium salt solution in the middle period is respectively applied to the deep soil layer and the surface of the soil by matching with straw powder after pyrolysis, the acidity of the deep soil is neutralized for a long time in the middle period, the magnesium salt solution is supplemented by drip irrigation in the later period, the effective magnesium content of the soil is maintained for a long time, meanwhile, the formation of agglomerates is promoted while the earthworms are added to loosen the soil, the problem that carbon fixation and emission reduction can be realized in the acid soil continuously in the short period, the middle period and the long period is solved, and the problem that the single application of lime cannot take effect for a long time and secondary acidizing is easy is solved.|DRAWINGS DESCRIPTION|[0018] FIG. 1 is a flow chart of the steps of the present invention.|INVENTION MODE|Detailed Description|[0019] The present invention will be further described in detail with reference to the following examples, which are only for the purpose of illustrating the invention and are not to be construed as limiting the scope of the invention.|[0020] Straw is a generic term for the stem and leaf parts of mature crops. Straw generally refers to the remainder of wheat, rice, corn, potatoes, rape, cotton, sugarcane and other crops after harvesting the seeds, more than half of the crop photosynthesis products being present in the straw. The straw is rich in nitrogen, phosphorus, potassium, calcium, magnesium, organic matters and the like, and is a renewable biological resource with multiple purposes. The straw is also a coarse fodder, and is characterized by high coarse fiber content and lignin. The straw is used as an important resource of agricultural wastes, has multidimensional utilization value, and can increase soil organic matters, improve aggregate structure, promote water and fertilizer retention capacity and promote microbial activity after returning to the field. The resource efficient conversion is realized through feed conversion, energy conversion, base material conversion and raw material conversion.|[0021] Example 1|[0022] Based on this, according to the illustration in fig. 1, the embodiment provides an innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil, which comprises the following steps:|[0023] firstly, preprocessing straws, namely cleaning and drying the straws, crushing the straws to the particle size of 0.2mm, and filtering the straws through a 20-mesh nylon sieve to obtain uniform straw powder; |[0024] The method comprises the steps of cleaning and removing soil, sand and stone and microorganism pollutants on the surface of the straw, avoiding the interference of impurities with the subsequent modification and pyrolysis processes, drying the straw, reducing the water content of the straw to below 10%, preventing heat loss and uneven products caused by water evaporation during pyrolysis, crushing and screening the straw to increase the contact area of the straw and magnesium salt solution, improving the impregnation efficiency, ensuring uniform heating during pyrolysis, and avoiding the problem of insufficient reaction inside large-particle straw. The pretreated straw has higher purity and uniform granularity, provides an ideal reaction substrate for subsequent magnesium salt modification, enables magnesium ions to fully permeate into the pores inside the straw, obviously improves the loading uniformity and quality stability of the modified biochar, reduces energy consumption in the pyrolysis process by drying and crushing, and improves the biochar yield of the straw per unit mass. |[0025] Step two, preparing charcoal by modifying straw, namely mixing the straw powder obtained in the step one with a magnesium salt solution at a rotating speed of 500-800 rpm, and preparing magnesium modified biochar by using a slow pyrolysis method;|[0026] the slow pyrolysis method is to heat to 500 ℃ in a tube furnace at a temperature rising speed of 5 ℃ per minute to carry out oxygen-limited slow pyrolysis, and the carbonization reaction is completed after heat preservation for 2 hours. The concentration of the magnesium salt solution is 0.1mol/L, and the mass ratio of the straw powder to the solution is 1:10. The magnesium salt solution promotes magnesium ions to adsorb hydroxyl and carboxyl functional groups on the surface of the straw through ion exchange, so as to form a stable magnesium-organic compound. The deep cracking of cellulose and hemicellulose in the straw is further promoted by oxygen limiting pyrolysis, a stable carbon structure rich in aromatic rings is generated, magnesium ions are promoted to react with oxides on the surface of the carbon to generate mineral phases such as magnesium oxide and the like, and the mineral phases are fully embedded into the porous framework of the biochar. |[0027] Thirdly, lime neutralization, lime is applied to the soil, and the lime application amount is 2 tons/hectare;|[0028] the lime is utilized to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, so that the pH value of the soil is directly improved, the toxicity of soil acidification to crop root systems is relieved, the advantage of quick effect of lime neutralization is fully utilized, the problem of soil acidification is relieved in a short period, and meanwhile, the lime raw material is low in price and high in economic feasibility. |[0029] Mixing and deeply burying, namely mixing the magnesium modified biochar prepared in the second step with the unmodified straw powder in the first step, injecting the mixture into the deep soil of 20cm, reducing microbial decomposition of organic carbon by utilizing the low-oxygen environment and the characteristic of low microbial activity of the deep soil, and covering the surface layer of the soil with the unmodified straw powder in the first step to form a physical barrier layer on the surface so as to further isolate air permeation, thereby realizing the combination of deep application and surface layer coverage and avoiding single improvement;|[0030] the mass ratio of the magnesium modified biochar to the straw powder is 1:3, and the application amount is 5 tons/hectare. Through physical and chemical synergistic effect, the carbon sequestration efficiency is obviously improved and the soil microenvironment is optimized. Straw powder is used as loose organic materials to be mixed with magnesium modified biochar to fill biochar pores, a carbon-straw composite layer is formed in deep soil, air diffusion is blocked, and the availability of microorganisms to the organic carbon is reduced. |[0031] And fifthly, later-stage regulation and control, supplementing magnesium salt solution into the soil by adopting a drip irrigation mode, and synchronously adding earthworms into the soil.|[0032] The concentration of the magnesium salt solution for drip irrigation is 0.5mol/L, and 1.3L/m2 is supplemented once. The earthworm putting density is 600 strips/m 2, and the repairing period is 15 days. Magnesium ions lost due to rain leaching or crop absorption are supplemented by drip irrigation of the magnesium salt solution periodically, so that the long-term inhibition effect of the magnesium salt on soil acidification is ensured. The soil aggregate formation is promoted by the feeding and excreting activities of the earthworms put in.|[0033] Example 2|[0034] According to the embodiment shown in fig. 1, an innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil is provided, which comprises the following steps:|[0035] firstly, preprocessing straws, namely cleaning and drying the straws, crushing the straws to the particle size of 0.3mm, and filtering the crushed straws by a 20-mesh nylon sieve to obtain uniform straw powder; |[0036] The method comprises the steps of cleaning and removing soil, sand and stone and microorganism pollutants on the surface of the straw, avoiding the interference of impurities with the subsequent modification and pyrolysis processes, drying the straw, reducing the water content of the straw to below 10%, preventing heat loss and uneven products caused by water evaporation during pyrolysis, crushing and screening the straw to increase the contact area of the straw and magnesium salt solution, improving the impregnation efficiency, ensuring uniform heating during pyrolysis, and avoiding the problem of insufficient reaction inside large-particle straw. The pretreated straw has higher purity and uniform granularity, provides an ideal reaction substrate for subsequent magnesium salt modification, enables magnesium ions to fully permeate into the pores inside the straw, obviously improves the loading uniformity and quality stability of the modified biochar, reduces energy consumption in the pyrolysis process by drying and crushing, and improves the biochar yield of the straw per unit mass. |[0037] Step two, preparing charcoal by modifying straw, namely mixing straw powder obtained in the step one with magnesium salt solution at a rotating speed of 800rpm, and preparing magnesium modified biochar by a slow pyrolysis method;|[0038] The slow pyrolysis method is to heat to 500 ℃ in a tube furnace at a temperature rising speed of 5 ℃ per minute to carry out oxygen-limited slow pyrolysis, and the carbonization reaction is completed after 3 hours of heat preservation. The concentration of the magnesium salt solution is 0.9mol/L, and the mass ratio of the straw powder to the solution is 1:20. The magnesium salt solution promotes magnesium ions to adsorb hydroxyl and carboxyl functional groups on the surface of the straw through ion exchange, so as to form a stable magnesium-organic compound. The deep cracking of cellulose and hemicellulose in the straw is further promoted by oxygen limiting pyrolysis, a stable carbon structure rich in aromatic rings is generated, magnesium ions are promoted to react with oxides on the surface of the carbon to generate mineral phases such as magnesium oxide and the like, and the mineral phases are fully embedded into the porous framework of the biochar. |[0039] Thirdly, lime neutralization, lime is applied to the soil, and the lime application amount is 4 tons/hectare;|[0040] the lime is utilized to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, so that the pH value of the soil is directly improved, the toxicity of soil acidification to crop root systems is relieved, the advantage of quick effect of lime neutralization is fully utilized, the problem of soil acidification is relieved in a short period, and meanwhile, the lime raw material is low in price and high in economic feasibility. |[0041] Mixing and deeply burying, namely mixing the magnesium modified biochar prepared in the second step with the unmodified straw powder in the first step, injecting the mixture into the underground soil for deep layer 30cm, reducing microbial decomposition of organic carbon by utilizing the low-oxygen environment and low microbial activity of deep soil, covering the surface layer of the soil with the unmodified straw powder in the first step, forming a physical barrier layer on the surface, further isolating air permeation, and realizing combination of deep application and surface layer coverage to avoid single improvement;|[0042] The mass ratio of the magnesium modified biochar to the straw powder is 1:3, and the application amount is 8 tons/hectare. Through physical and chemical synergistic effect, the carbon sequestration efficiency is obviously improved and the soil microenvironment is optimized. Straw powder is used as loose organic materials to be mixed with magnesium modified biochar to fill biochar pores, a carbon-straw composite layer is formed in deep soil, air diffusion is blocked, and the availability of microorganisms to the organic carbon is reduced. |[0043] And fifthly, later-stage regulation and control, supplementing magnesium salt solution into the soil by adopting a drip irrigation mode, and synchronously adding earthworms into the soil.|[0044] The concentration of the magnesium salt solution for drip irrigation is 0.7mol/L, and 2L/m2 is supplemented once. The earthworm putting density is 800 strips/m 2, and the repairing period is 20 days. Magnesium ions lost due to rain leaching or crop absorption are supplemented by drip irrigation of the magnesium salt solution periodically, so that the long-term inhibition effect of the magnesium salt on soil acidification is ensured. The soil aggregate formation is promoted by the feeding and excreting activities of the earthworms put in.|[0045] When the innovative application method for realizing carbon fixation and emission reduction of the acid soil is used, the straw is cleaned, dried and crushed, then mixed and impregnated with the magnesium salt solution to realize the full combination of magnesium ions and functional groups on the surface of the straw, then the impregnated straw is pyrolyzed and modified to generate magnesium modified biochar with larger specific surface area, and a large amount of magnesium oxide is loaded by utilizing the porous structure of the magnesium modified biochar. Lime is firstly applied to acid soil, the problem of soil acidification is effectively relieved by neutralization reaction in a short period of time, then the lime is applied to the soil in a layered manner, a mixture of magnesium modified biochar and unmodified straw is embedded into deep soil, straw powder is covered on the surface layer, and a composite layer physical barrier is constructed. The surface layer straw is decomposed to generate organic acid which is neutralized by the alkaline environment modified by the magnesium modified biochar, so that the local acidification rebound of soil is avoided. The method realizes long-time neutralization of the acidity of deep soil in the middle stage, improves the carbon sequestration stability, adopts a drip irrigation mode to periodically supplement magnesium salt solution in the later stage, maintains the effective magnesium content of the soil, and promotes the formation of agglomerates by matching with the addition of earthworms.|[0046] The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof. (CN121241723)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of agricultural ecology, in particular to an innovative application method for realizing carbon fixation and emission reduction of straws in acid soil.|BACKGROUND ART|[0002] Soil is the most important carbon reservoir of the land ecological system, the carbon reservoir amount is about 3 times of the atmosphere, soil carbon sequestration is recognized as the most potential, lowest cost and most easy to operate and realize technical approach, the reduction of carbon emission in the atmosphere and the reduction of greenhouse gas emission are one of important ecological tasks for coping with global climate change, while the agriculture and forestry ecological system plays an important role in carbon sequestration and emission reduction, the carbon sequestration capacity of the agriculture and forestry ecological system is enhanced mainly by increasing the organic carbon reserves and reducing the decomposition of organic carbon, the global carbon emission can be slowed down to a certain extent, and the acid soil carbon sequestration and emission reduction is a technical system for improving the carbon sequestration capacity of the soil and reducing the greenhouse gas emission through physical-chemical-biological synergism. The core is to utilize biochar (such as straw carbonized products) and mineral materials (such as oyster shells and wollastonite) to improve the acidity of soil.|[0003] The invention patent with the application number 202311059727.2 discloses a method for improving the utilization rate of microbial carbon in acid soil by applying lime to straw returning fields, which comprises the steps of firstly applying lime to soil, on one hand, fully neutralizing hydrogen ions in the soil by the lime, increasing the pH of the soil, on the other hand, activating microorganisms and eliminating external interference as much as possible, and then crushing the straw and returning the crushed straw to fields. The straw returning and lime applying method can obviously improve the utilization efficiency of the microbial carbon in the acid soil;|[0004] However, in the method for improving the utilization rate of the microbial carbon in the acid soil by using the lime in the straw returning field, under the traditional returning field mode, the decomposition rate of the straw is higher, the loss of active organic carbon is easy to cause, and the long-term carbon fixing effect cannot be ensured. |DISCLOSURE|Disclosure of Invention|[0005] Aiming at the problems, the invention aims to provide an innovative application method for realizing carbon fixation and emission reduction of straws in acid soil, which realizes the short-term alleviation of the problem of acidified soil by applying lime on the soil to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, fully utilizes the advantage of quick effect of lime neutralization, and adopts the method that magnesium modified biochar prepared by crushing and soaking the straws in a magnesium salt solution in the middle stage is respectively applied on the deep soil layer and the surface of the soil to realize the long-term neutralization of the deep soil acidity, adopts drip irrigation to supplement the magnesium salt solution in the later stage to realize the long-term maintenance of the effective magnesium content of the soil, and simultaneously promotes the formation of agglomerates when being matched with the addition of earthworms to loosen the soil, thereby realizing the long-term carbon fixation and emission reduction in the acid soil continuously in the short-term, middle-term and long-term, and effectively solving the problems that the single application of lime cannot realize long-term effect and secondary acidification is easy to cause.|[0006] The invention aims at realizing the purposes by adopting the following technical scheme that the innovative application method for realizing carbon fixation and emission reduction of the straw in the acid soil comprises the following steps:|[0007] Firstly, preprocessing straws, namely cleaning and drying the straws, crushing the straws to the particle size of 0.1-0.3 mm, and filtering the crushed straws by a 20-mesh nylon screen to obtain uniform straw powder; |[0008] step two, preparing charcoal by modifying straw, namely mixing the straw powder obtained in the step one with a magnesium salt solution at a rotating speed of 500-800 rpm, and preparing magnesium modified biochar by using a slow pyrolysis method; |[0009] Thirdly, lime neutralization, lime is applied to the soil, and the lime application amount is 2-4 tons/hectare; |[0010] Step four, mixing and deep burying, namely mixing the magnesium modified biochar prepared in the step two with the unmodified straw powder in the step one, injecting the mixture into the deep soil layer of 20-30 cm underground, and covering the unmodified straw powder in the step one on the surface layer of the soil; |[0011] And fifthly, later-stage regulation and control, supplementing magnesium salt solution into the soil by adopting a drip irrigation mode, and synchronously adding earthworms into the soil. |[0012] The further improvement is that the concentration of the magnesium salt solution in the second step is 0.05-0.9 mol/L, and the mass ratio of the straw powder to the solution is 1:5-1:20.|[0013] The further improvement is that the slow pyrolysis method in the second step is to heat to 500 ℃ in a tube furnace at a temperature rising speed of 5 ℃ per minute for oxygen-limited slow pyrolysis, and the carbonization reaction is completed after heat preservation for 1-3 hours.|[0014] The method is further improved in that in the fourth step, the mass ratio of the magnesium modified biochar to the straw powder is 1:3, and the application amount is 5-8 tons/hectare.|[0015] The further improvement is that the concentration of the magnesium salt solution for drip irrigation in the fifth step is 0.3-0.7 mol/L, and 1-2L/m < 2 > is supplemented once.|[0016] The method is further improved in that the earthworm putting density in the fifth step is 500-800 strips/m < 2 >, and the repairing period is 15-20 days.|[0017] The invention has the beneficial effects that lime is applied to soil to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, so that the problem of acidizing the soil in a short period is solved, the advantage of quick neutralization effect of lime is fully utilized, the magnesium modified biochar prepared by crushing and soaking the straw in the magnesium salt solution in the middle period is respectively applied to the deep soil layer and the surface of the soil by matching with straw powder after pyrolysis, the acidity of the deep soil is neutralized for a long time in the middle period, the magnesium salt solution is supplemented by drip irrigation in the later period, the effective magnesium content of the soil is maintained for a long time, meanwhile, the formation of agglomerates is promoted while the earthworms are added to loosen the soil, the problem that carbon fixation and emission reduction can be realized in the acid soil continuously in the short period, the middle period and the long period is solved, and the problem that the single application of lime cannot take effect for a long time and secondary acidizing is easy is solved.|DRAWINGS DESCRIPTION|[0018] FIG. 1 is a flow chart of the steps of the present invention.|INVENTION MODE|Detailed Description|[0019] The present invention will be further described in detail with reference to the following examples, which are only for the purpose of illustrating the invention and are not to be construed as limiting the scope of the invention.|[0020] Straw is a generic term for the stem and leaf parts of mature crops. Straw generally refers to the remainder of wheat, rice, corn, potatoes, rape, cotton, sugarcane and other crops after harvesting the seeds, more than half of the crop photosynthesis products being present in the straw. The straw is rich in nitrogen, phosphorus, potassium, calcium, magnesium, organic matters and the like, and is a renewable biological resource with multiple purposes. The straw is also a coarse fodder, and is characterized by high coarse fiber content and lignin. The straw is used as an important resource of agricultural wastes, has multidimensional utilization value, and can increase soil organic matters, improve aggregate structure, promote water and fertilizer retention capacity and promote microbial activity after returning to the field. The resource efficient conversion is realized through feed conversion, energy conversion, base material conversion and raw material conversion.|[0021] Example 1|[0022] Based on this, according to the illustration in fig. 1, the embodiment provides an innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil, which comprises the following steps:|[0023] firstly, preprocessing straws, namely cleaning and drying the straws, crushing the straws to the particle size of 0.2mm, and filtering the straws through a 20-mesh nylon sieve to obtain uniform straw powder; |[0024] The method comprises the steps of cleaning and removing soil, sand and stone and microorganism pollutants on the surface of the straw, avoiding the interference of impurities with the subsequent modification and pyrolysis processes, drying the straw, reducing the water content of the straw to below 10%, preventing heat loss and uneven products caused by water evaporation during pyrolysis, crushing and screening the straw to increase the contact area of the straw and magnesium salt solution, improving the impregnation efficiency, ensuring uniform heating during pyrolysis, and avoiding the problem of insufficient reaction inside large-particle straw. The pretreated straw has higher purity and uniform granularity, provides an ideal reaction substrate for subsequent magnesium salt modification, enables magnesium ions to fully permeate into the pores inside the straw, obviously improves the loading uniformity and quality stability of the modified biochar, reduces energy consumption in the pyrolysis process by drying and crushing, and improves the biochar yield of the straw per unit mass. |[0025] Step two, preparing charcoal by modifying straw, namely mixing the straw powder obtained in the step one with a magnesium salt solution at a rotating speed of 500-800 rpm, and preparing magnesium modified biochar by using a slow pyrolysis method;|[0026] the slow pyrolysis method is to heat to 500 ℃ in a tube furnace at a temperature rising speed of 5 ℃ per minute to carry out oxygen-limited slow pyrolysis, and the carbonization reaction is completed after heat preservation for 2 hours. The concentration of the magnesium salt solution is 0.1mol/L, and the mass ratio of the straw powder to the solution is 1:10. The magnesium salt solution promotes magnesium ions to adsorb hydroxyl and carboxyl functional groups on the surface of the straw through ion exchange, so as to form a stable magnesium-organic compound. The deep cracking of cellulose and hemicellulose in the straw is further promoted by oxygen limiting pyrolysis, a stable carbon structure rich in aromatic rings is generated, magnesium ions are promoted to react with oxides on the surface of the carbon to generate mineral phases such as magnesium oxide and the like, and the mineral phases are fully embedded into the porous framework of the biochar. |[0027] Thirdly, lime neutralization, lime is applied to the soil, and the lime application amount is 2 tons/hectare;|[0028] the lime is utilized to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, so that the pH value of the soil is directly improved, the toxicity of soil acidification to crop root systems is relieved, the advantage of quick effect of lime neutralization is fully utilized, the problem of soil acidification is relieved in a short period, and meanwhile, the lime raw material is low in price and high in economic feasibility. |[0029] Mixing and deeply burying, namely mixing the magnesium modified biochar prepared in the second step with the unmodified straw powder in the first step, injecting the mixture into the deep soil of 20cm, reducing microbial decomposition of organic carbon by utilizing the low-oxygen environment and the characteristic of low microbial activity of the deep soil, and covering the surface layer of the soil with the unmodified straw powder in the first step to form a physical barrier layer on the surface so as to further isolate air permeation, thereby realizing the combination of deep application and surface layer coverage and avoiding single improvement;|[0030] the mass ratio of the magnesium modified biochar to the straw powder is 1:3, and the application amount is 5 tons/hectare. Through physical and chemical synergistic effect, the carbon sequestration efficiency is obviously improved and the soil microenvironment is optimized. Straw powder is used as loose organic materials to be mixed with magnesium modified biochar to fill biochar pores, a carbon-straw composite layer is formed in deep soil, air diffusion is blocked, and the availability of microorganisms to the organic carbon is reduced. |[0031] And fifthly, later-stage regulation and control, supplementing magnesium salt solution into the soil by adopting a drip irrigation mode, and synchronously adding earthworms into the soil.|[0032] The concentration of the magnesium salt solution for drip irrigation is 0.5mol/L, and 1.3L/m2 is supplemented once. The earthworm putting density is 600 strips/m 2, and the repairing period is 15 days. Magnesium ions lost due to rain leaching or crop absorption are supplemented by drip irrigation of the magnesium salt solution periodically, so that the long-term inhibition effect of the magnesium salt on soil acidification is ensured. The soil aggregate formation is promoted by the feeding and excreting activities of the earthworms put in.|[0033] Example 2|[0034] According to the embodiment shown in fig. 1, an innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil is provided, which comprises the following steps:|[0035] firstly, preprocessing straws, namely cleaning and drying the straws, crushing the straws to the particle size of 0.3mm, and filtering the crushed straws by a 20-mesh nylon sieve to obtain uniform straw powder; |[0036] The method comprises the steps of cleaning and removing soil, sand and stone and microorganism pollutants on the surface of the straw, avoiding the interference of impurities with the subsequent modification and pyrolysis processes, drying the straw, reducing the water content of the straw to below 10%, preventing heat loss and uneven products caused by water evaporation during pyrolysis, crushing and screening the straw to increase the contact area of the straw and magnesium salt solution, improving the impregnation efficiency, ensuring uniform heating during pyrolysis, and avoiding the problem of insufficient reaction inside large-particle straw. The pretreated straw has higher purity and uniform granularity, provides an ideal reaction substrate for subsequent magnesium salt modification, enables magnesium ions to fully permeate into the pores inside the straw, obviously improves the loading uniformity and quality stability of the modified biochar, reduces energy consumption in the pyrolysis process by drying and crushing, and improves the biochar yield of the straw per unit mass. |[0037] Step two, preparing charcoal by modifying straw, namely mixing straw powder obtained in the step one with magnesium salt solution at a rotating speed of 800rpm, and preparing magnesium modified biochar by a slow pyrolysis method;|[0038] The slow pyrolysis method is to heat to 500 ℃ in a tube furnace at a temperature rising speed of 5 ℃ per minute to carry out oxygen-limited slow pyrolysis, and the carbonization reaction is completed after 3 hours of heat preservation. The concentration of the magnesium salt solution is 0.9mol/L, and the mass ratio of the straw powder to the solution is 1:20. The magnesium salt solution promotes magnesium ions to adsorb hydroxyl and carboxyl functional groups on the surface of the straw through ion exchange, so as to form a stable magnesium-organic compound. The deep cracking of cellulose and hemicellulose in the straw is further promoted by oxygen limiting pyrolysis, a stable carbon structure rich in aromatic rings is generated, magnesium ions are promoted to react with oxides on the surface of the carbon to generate mineral phases such as magnesium oxide and the like, and the mineral phases are fully embedded into the porous framework of the biochar. |[0039] Thirdly, lime neutralization, lime is applied to the soil, and the lime application amount is 4 tons/hectare;|[0040] the lime is utilized to neutralize hydrogen ions and exchangeable aluminum ions in the soil to play a role, so that the pH value of the soil is directly improved, the toxicity of soil acidification to crop root systems is relieved, the advantage of quick effect of lime neutralization is fully utilized, the problem of soil acidification is relieved in a short period, and meanwhile, the lime raw material is low in price and high in economic feasibility. |[0041] Mixing and deeply burying, namely mixing the magnesium modified biochar prepared in the second step with the unmodified straw powder in the first step, injecting the mixture into the underground soil for deep layer 30cm, reducing microbial decomposition of organic carbon by utilizing the low-oxygen environment and low microbial activity of deep soil, covering the surface layer of the soil with the unmodified straw powder in the first step, forming a physical barrier layer on the surface, further isolating air permeation, and realizing combination of deep application and surface layer coverage to avoid single improvement;|[0042] The mass ratio of the magnesium modified biochar to the straw powder is 1:3, and the application amount is 8 tons/hectare. Through physical and chemical synergistic effect, the carbon sequestration efficiency is obviously improved and the soil microenvironment is optimized. Straw powder is used as loose organic materials to be mixed with magnesium modified biochar to fill biochar pores, a carbon-straw composite layer is formed in deep soil, air diffusion is blocked, and the availability of microorganisms to the organic carbon is reduced. |[0043] And fifthly, later-stage regulation and control, supplementing magnesium salt solution into the soil by adopting a drip irrigation mode, and synchronously adding earthworms into the soil.|[0044] The concentration of the magnesium salt solution for drip irrigation is 0.7mol/L, and 2L/m2 is supplemented once. The earthworm putting density is 800 strips/m 2, and the repairing period is 20 days. Magnesium ions lost due to rain leaching or crop absorption are supplemented by drip irrigation of the magnesium salt solution periodically, so that the long-term inhibition effect of the magnesium salt on soil acidification is ensured. The soil aggregate formation is promoted by the feeding and excreting activities of the earthworms put in.|[0045] When the innovative application method for realizing carbon fixation and emission reduction of the acid soil is used, the straw is cleaned, dried and crushed, then mixed and impregnated with the magnesium salt solution to realize the full combination of magnesium ions and functional groups on the surface of the straw, then the impregnated straw is pyrolyzed and modified to generate magnesium modified biochar with larger specific surface area, and a large amount of magnesium oxide is loaded by utilizing the porous structure of the magnesium modified biochar. Lime is firstly applied to acid soil, the problem of soil acidification is effectively relieved by neutralization reaction in a short period of time, then the lime is applied to the soil in a layered manner, a mixture of magnesium modified biochar and unmodified straw is embedded into deep soil, straw powder is covered on the surface layer, and a composite layer physical barrier is constructed. The surface layer straw is decomposed to generate organic acid which is neutralized by the alkaline environment modified by the magnesium modified biochar, so that the local acidification rebound of soil is avoided. The method realizes long-time neutralization of the acidity of deep soil in the middle stage, improves the carbon sequestration stability, adopts a drip irrigation mode to periodically supplement magnesium salt solution in the later stage, maintains the effective magnesium content of the soil, and promotes the formation of agglomerates by matching with the addition of earthworms.|[0046] The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof. Family Number|(117291810)|117291810|Abstract|(CN121241723 A)|The invention discloses an innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil , which comprises the following steps : step 1, straw pretreatment : cleaning , drying and crushing the straw to obtain straw powder ; 2, straw modification for carbon preparation , wherein straw powder and a magnesium salt solution are mixed , and magnesium modified biochar is prepared through a low - speed pyrolysis method ; step 3, lime neutralization : lime is applied to the soil ; step 4, mixing and deep burying : mixing the magnesium modified biochar and unmodified straw powder , injecting the mixture into the deep layer of the underground soil , and covering the unmodified straw powder in the step 1 on the surface layer of the soil ; 5, later regulation and control , wherein a magnesium salt solution is supplemented in a drip irrigation mode ; lime is applied to the soil to neutralize the soil , in the middle stage , the magnesium modified biochar prepared through straw pyrolysis is matched with straw powder to be applied to the deep layer and the surface of the soil respectively , in the later stage , a magnesium salt solution is supplemented through drip irrigation , the effective magnesium content of the soil is maintained for a long time , and short - term , middle - term and long - term continuous carbon sequestration and emission reduction are achieved . |CPC codes|(CN121241723 A)|A01B - 079/00 |A01B - 079/02 |A01K - 067/033/2 |IPC codes|(CN121241723 A)|A01B - 079/00 |A01K - 067/33 |Title|(CN121241723 A)|Innovative application method for realizing carbon sequestration and emission reduction of straws in acid soil | Basic materials chemistry|Other special machines A01B-079/00|A01B-079/02|A01K-067/033/2|C05D-009/00|C05G-003/00|C05G-003/80|C09K-017/02|C09K-017/32|C09K-017/40|C09K-2101/00 A01B-079/00|A01B-079/02|A01K-067/033/2|C05D-009/00|C05G-003/00|C05G-003/80|C09K-017/02|C09K-017/32|C09K-017/40|C09K-2101/00 A01B-079/00|A01K-067/33|C09K-017/02|C09K-017/40|C09K-101/00 A01B-079/00|A01K-067/33|C09K-017/02|C09K-017/40|C09K-101/00 PENDING (CN121241723)|PENDING ALIVE (CN121241723)|ALIVE (CN121241723)|LEGAL DETAILS FOR CN121241723|Actual or expected expiration date=2045-09-28|Legal state=ALIVE|Status=PENDING|Event publication date=2025-09-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511396551|Application date=2025-09-28|Standardized application number=2025CN-1396551|Event publication date=2026-01-02|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121241723|Publication stage code=A|Publication date=2026-01-02|Standardized publication number=CN121241723|Event publication date=2026-01-02|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2026-01-20|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121241723)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKf3p6UEJHxW0lfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080341178&ekey=2276&xpn=CN121241723&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252Fp%252FVYy7oKp2%252BhJRe3y2pT5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121241723)|CN (CN121241723)|NAME=GUANGDONG ACADEMY OF AGRICULTURAL SCIENCES, INSTITUTE OF AGRICULTURAL RESOURCES AND ENVIRONMENT , COUNTRY=CN (CN121241723)|NAME=WANG YONGZE;BEIJING SHENGGUANGXINHE IP FIRM , REG=16117 (CN121241723)|CN (CN121241723)|NAME=HUANG QIAOYI, COUNTRY=CN |NAME=TANG SHUANHU|NAME=HUANG XU|NAME=HUANG JIANFENG|NAME=WU TENGFEI|NAME=ZHANG MU|NAME=YI QIONG|NAME=PANG YUWAN|NAME=DING WUHAN|NAME=CENG KE|NAME=WU YONGPEI|NAME=LI PING|NAME=FU HONGTING|NAME=LUO HAIBIN 0 1 Titre: (CN121241723)|Innovative application method for realizing carbon sequestration and emission reduction of straws in acid soil Résumé: (CN121241723)|The invention discloses an innovative application method for realizing carbon sequestration and emission reduction of straw in acid soil, which comprises the following steps: step 1, straw pretreatment: cleaning, drying and crushing the straw to obtain straw powder; 2, straw modification for carbon preparation, wherein straw powder and a magnesium salt solution are mixed, and magnesium modified biochar is prepared through a low-speed pyrolysis method; step 3, lime neutralization: lime is applied to the soil; step 4, mixing and deep burying: mixing the magnesium modified biochar and unmodified straw powder, injecting the mixture into the deep layer of the underground soil, and covering the unmodified straw powder in the step 1 on the surface layer of the soil; 5, later regulation and control, wherein a magnesium salt solution is supplemented in a drip irrigation mode; lime is applied to the soil to neutralize the soil, in the middle stage, the magnesium modified biochar prepared through straw pyrolysis is matched with straw powder to be applied to the deep layer and the surface of the soil respectively, in the later stage, a magnesium salt solution is supplemented through drip irrigation, the effective magnesium content of the soil is maintained for a long time, and short-term, middle-term and long-term continuous carbon sequestration and emission reduction are achieved. 40 Abstract gpt-4o-mini no The article focuses on carbon sequestration using straw and magnesium salts in soil, without discussing mineral weathering or the use of silicate minerals for CO₂ capture.
44 CN202510226727 CN202510226727 CN119951390|CN119951390 114513321 CN119951390 B 2025-11-18 [CN119951390B]|CN119951390 A 2025-05-09 [CN119951390] 2025-02-27 2025-02-27 2025-11-18|2025-05-09 (CN119951390B)|2025-11-18 (CN119951390)|2045-02-27 (CN119951390)|SC-CO-based2Method for preparing paste filling body with carbon fixation and energy absorption functions through foaming (CN119951390)|The invention discloses a method for preparing a paste filling body with carbon sequestration and energy absorption functions based on SC-CO2 foaming, and belongs to the technical field of coal mining. The preparation method comprises the following steps: crushing and grinding a coal-based solid waste raw material, and stirring and mixing the crushed and ground coal-based solid waste raw material with mixing water at a speed of less than 60r/min to prepare coal-based solid waste slurry; cO2 in a supercritical state is continuously injected during stirring until the pressure is the same as the set pressure, the supercritical CO2 permeates into the coal-based solid waste material slurry to form a mixture of the supercritical CO2 and the coal-based solid waste material slurry, the mixture of the supercritical CO2 and the coal-based solid waste material slurry is stirred and mixed in a turbo mode to form foam paste filling body master batch, and the foam paste filling body master batch is formed. The heat preservation and the pressure maintaining of the foam paste filling body master batch are controlled in a high-temperature and high-pressure mixer for 10-30 minutes, and then the pressure is quickly relieved, so that a large number of coal-based solid waste foam paste filling bodies taking supercritical CO2 as foam nucleuses are formed, the foaming of the paste filling body master batch is realized, and the filling body has low density, good heat insulation performance and a controllable foam pore structure. SHANDONG GOLD MINING TECHNOLOGY|XI AN UNIVERSITY OF SCIENCE & TECHNOLOGY (CN119951390)|XI'AN UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN])|SHANDONG GOLD MINING TECHNOLOGY CO., LTD.|(CN119951390)|XI'AN UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN])|SHANDONG GOLD MINING TECHNOLOGY CO., LTD. YAN BAOXU|LIU PENGHAO|WANG ZEHANG|WANG BO|HE XIA|LIU YULIANG|JIA HANWEN (CN119951390)|YAN BAOXU|LIU PENGHAO|WANG ZEHANG|WANG BO|HE XIA|LIU YULIANG|JIA HANWEN|(CN119951390)|YAN BAOXU|LIU PENGHAO|WANG ZEHANG|WANG BO|HE XIA|LIU YULIANG|JIA HANWEN (CN119951390)|JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 61223 (CN119951390)|The paste filling body with the carbon fixation and energy absorption functions prepared by the preparation method disclosed by the invention has the advantages of excellent performance, low density, light weight, high compression resistance, good heat insulation performance and controllable cell structure, can be used for a long time under various extreme environmental conditions, and is suitable for actual requirements of mine dynamic environment and dynamic disaster prevention and control.|Compared with the prior art, the method has the beneficial effects that the coal-based solid waste raw material is crushed and ground into fine particles with the particle size smaller than 20 mu m, meanwhile, in the process of preparing the coal-based solid waste slurry, air mixing can be avoided by adopting a low-speed stirring mode, meanwhile, when the prepared coal-based solid waste slurry is injected with supercritical CO _2, the supercritical CO _2 is injected while stirring at high temperature and high pressure, the supercritical CO _2 can be fully permeated into the coal-based solid waste slurry to form a mixture of the supercritical CO _2 and the coal-based solid waste slurry, and meanwhile, the mixture of the supercritical CO _2 and the coal-based solid waste slurry is mixed and stirred at high temperature and high pressure, so that the problems that the coal-based solid waste slurry is compacted, the pore forming is difficult and a foaming paste filling body cannot be formed due to high pressure are avoided when the supercritical carbon dioxide is injected into the coal-based solid waste slurry.|The preparation of the traditional filling material with the carbon fixing function needs to consume a great deal of time and resources, a great deal of carbon dioxide is usually generated in the manufacturing process, the traditional filling material mainly uses cement and gangue or waste stone as basic materials, the density is high, the energy absorbing capacity is poor, and the requirements of high compression resistance and high energy absorption required by the prevention and control of mining dynamic disasters are difficult to meet. The existing paste filling material has obvious defects in the aspects of light weight, heat insulation and the like, and is difficult to adapt to the actual requirements of mine dynamic environment and dynamic disaster prevention and control.Disclosure of InventionThe invention aims to overcome the problems in the prior art, and provides the paste filling body prepared by the method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO _2 foaming, which has low density, high strength, good heat insulation performance and controllable cell structure, can be used for a long time under various extreme environmental conditions, and can better adapt to the actual requirements of mine dynamic environment and dynamic disaster prevention and control.|The terms "first," "second," and the like, as used in this disclosure, do not denote any order, quantity, or importance, but rather are used to distinguish one element from another.| (CN119951390)|1. The method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming is characterized by comprising the following steps of: crushing and grinding the coal-based solid waste raw materials, and stirring and mixing the crushed and ground coal-based solid waste raw materials with mixing water at a speed of less than 60r/min to prepare coal-based solid waste slurry, wherein particles with a particle size of less than 20 mu m account for more than 15% in powder formed by crushing and grinding the coal-based solid waste raw materials; The prepared coal-based solid waste slurry is injected into a preheated high-temperature high-pressure mixer for stirring, and supercritical CO 2 is continuously injected in the stirring process, wherein the injection volume of the coal-based solid waste slurry is 1/3-1/2 of the volume of the high-temperature high-pressure mixer, so that the supercritical CO 2 fully permeates with the coal-based solid carbon slurry in the high-temperature high-pressure mixer to give enough space to form a uniform cell structure, the temperature of the high-temperature high-pressure mixer is kept above 31 ℃, the pressure is kept above 7.3 MPa, so that the supercritical CO 2 is kept in a supercritical stable state at high temperature and high pressure in the high-temperature high-pressure mixer and fully permeates into the coal-based solid waste slurry to form a mixture of the supercritical CO 2 and the coal-based solid waste slurry; The method comprises the steps of mixing and stirring supercritical CO 2 and coal-based solid waste slurry mixture at high temperature and high pressure to form foam paste filler master batch, controlling the heat preservation and pressure maintaining time at high temperature and high pressure for 10-30min, then releasing pressure, and controlling the pressure maintaining time to prevent the coal-based solid waste slurry from pre-coagulating, so as to ensure sufficient fluidity of the coal-based solid waste slurry, controlling the pressure release speed to be 2.5MPa/s when the pressure of the foam paste filler master batch is released after Wen Baoya, gradually reducing the pressure in a high-temperature high-pressure mixer to be 0-7.4MPa, controlling the pressure release speed to be 2.5MPa/s, wherein the pressure release speed is not too fast, otherwise, CO 2 in the high-temperature high-pressure mixer generates dry ice, the foaming effect is influenced, and a large amount of paste with a carbon-fixing and energy-absorbing function taking supercritical CO 2 as a foam core is formed, and the stirring process is carried out under high-pressure high-temperature conditions, so that SC-CO 2 has higher diffusivity and permeability, and can rapidly permeate the coal-based solid waste slurry. | (CN119951390)|The invention discloses a method for preparing a paste filling body with carbon fixation and energy absorption functions based on SC-CO 2 foaming, and belongs to the technical field of coal mining.|The invention relates to a method for preparing a paste filling body with carbon fixation and energy absorption functions based on SC-CO _2 foaming, which comprises the following steps of crushing and grinding coal-based solid waste raw materials, stirring and mixing the crushed and ground coal-based solid waste raw materials with mixing water at a speed of less than 60r/min to prepare coal-based solid waste slurry;|The invention relates to the technical field of coal mining, in particular to a method for preparing a paste filling body with carbon fixation and energy absorption functions based on SC-CO _2 foaming.| (CN119951390)|PASTE FILLING(100,28)|CARBON FIXATION(100,26)|ENERGY ABSORPTION(100,22)|SC CO BASED2METHOD(100,1)|MINE DYNAMIC ENVIRONMENT REQUIREMENT(91,3)|MINE DYNAMIC ENVIRONMENT(82,3)|SOLID WASTE SLURRY(75,62)|DYNAMIC DISASTER PREVENTION(74,3)|CONSUME DEAL(52,1)|PASTE FILLER MASTER BATCH(48,2)|MASTER BATCH(46,8)|FOAMING PASTE FILLING(44,3)|SOLID WASTE(43,97)|PASTE FILLING MASTER BATCH(42,2)|COAL MINING(38,2)|MIXER(37,49)|CRUSHING(37,6)|SUPERCRITICAL STABLE(37,3)|DYNAMIC DISASTER(36,2)|LIGHTWEIGHT(35,2)|COMPRESSION RESISTANCE(33,3)|COAL SOLID CARBON SLURRY(32,2)|ENERGY ABSORPTION CAPACITY(32,1)|FOAM PASTE FILLER PRESSURE(32,1)|PASTE FILLER(31,5)|FLUIDITY(30,2)|FOAM PASTE FILLER(28,6)|PRESSURE RELEASE(28,2)|CARBON DIOXIDE DEAL(28,1)|HEAT PRESERVATION(27,4)|DIFFUSIVITY(27,3)|DEFECT(27,1)|SC CO(26,12)|MIXING WATER(25,6)|PERFORMING HEAT INSULATION(24,4)|ENERGY ABSORBING PASTE FILLER(23,2)|SOLID CARBON SLURRY(23,2)|GANGUE(23,1)|INJECTION VOLUME(21,3)|PERMEABILITY(21,3)|STIRRING(20,7)|FOAM CORE(19,3)|ENVIRONMENTAL CONDITION(19,2)|RELEASING PRESSURE(19,2)|CONTROLLABLE CELL STRUCTURE(17,2)|CARBON FIXING(16,6)|CEMENT(16,2)|PRESSURE RELEASE SPEED(15,1)|AIR MIXING(14,2)|FINE PARTICLE(14,1)|CARBON DIOXIDE(13,1)|RAW MATERIAL(12,14)|HEAT INSULATION(12,1)|SOLID WASTE RAW MATERIAL(11,14)|ENERGY ABSORPTION FUNCTION(11,10)|SUPERCRITICAL CARBON DIOXIDE(11,6)|ENERGY ABSORBING FUNCTION(11,3)|PARTICLE SIZE(11,3)|DRY ICE(11,2)|FILLING BODY MASTER BATCH(10,5)|MILITARY EXPLOSION PREVENTION(10,1)|OVERLYING MINING ROCK(10,1)|FILLING MATERIAL(9,4)|COAL GANGUE(9,2)|CONTROLLABLE FOAM CELL STRUCTURE(9,2)|CURED PASTE FILLING(9,2)|FOAM PASTE FILLING(9,2)|RAPID PRESSURE RELIEF(9,2)|CARBON FIXING FUNCTION(8,3)|CONVEYING VALVE(7,3)|FOAM NUCLEUS(7,2)|INORGANIC SUBSTANCE(7,2)|UNIFORM CELL STRUCTURE(7,2)|ATHLETE SOLE SHOCK ABSORPTION(7,1)|COAL EXPLOITATION(7,1)|FOAMING PASTE FILLER SLURRY(7,1)|LOOSE PASTE FILLING(7,1)|MINING PASTE FILLING(7,1)|MULTIDISASTER PREVENTION(7,1)|PREMATURE COAGULATION(7,1)|SLURRY RETURNING BLOCKAGE(7,1)|STRATEGY TRACTION(7,1)|SYNERGISTIC DISASTER PREVENTION(7,1)|PREPARATION EQUIPMENT(6,4)|CARBONIZATION REACTION(6,2)|DELIVERY VALVE(6,2)|POSITIONAL RELATIONSHIP(6,2)|COAL RESOURCE(6,1)|DIFFUSION PERMEATION(6,1)|HARMFUL BYPRODUCT(6,1)|POROSITY ANALYZER(6,1)|ROCK BURST(6,1)|TURBINE STIRRER(6,1)|PIPELINE(5,3)|SIGNIFICANCE(5,2)|3D MICROSCOPE(5,1)|CELL MORPHOLOGY(5,1)|CURING MAINTENANCE CHAMBER(5,1)|CURING OXIDATION CHAMBER(5,1)|DYNAMIC ADJUSTMENT PROPORTION(5,1)|FOAM FILLER POROSITY(5,1)|FUNDAMENTAL TRANSITION(5,1)|HIGH ENERGY ABSORPTION(5,1)|MINE ENVIRONMENT(5,1)|MINERALIZATION REACTION(5,1)|SOLIDIFIED FILLER COMPRESSIVE STRENGTH(5,1)|TURBINE STIRRING(5,1)|PRESSURE REACTOR(4,18)|SOLID WASTE FILLING(4,4)|PARTICLE RATIO(4,3)|STIRRING TIME(4,3)|COAL MINE(4,2)|NEGATIVE INFLUENCE(4,2)|BASIC MATERIAL(4,1)|BUBBLE CORE(4,1)|CARBON EXPLOITATION(4,1)|COAL DEVELOPMENT(4,1)|CURED COAL SOLID WASTE(4,1)|CURING CHAMBER(4,1)|DIFFUSION DISSOLUTION REACTION BEHAVIOR(4,1)|FACULTY(4,1)|FULL PERMEATION REACTION(4,1)|GREEN MINE CONSTRUCTION(4,1)|INJECTION COMPLETION(4,1)|ORDINARY MEANING(4,1)|PRESOLIDIFICATION(4,1)|SAFETY REQUIREMENT(4,1)|SLURRY INJECTION(4,1)|STIRRING DIFFICULTY(4,1)||(CN119951390)|CARBON FIXATION(100,30)|PASTE FILLING(100,30)|ENERGY ABSORPTION(100,25)|SC CO(100,15)|SC CO BASED2METHOD(100,1)|MINE DYNAMIC ENVIRONMENT REQUIREMENT(86,3)|MINE DYNAMIC ENVIRONMENT(77,3)|DYNAMIC DISASTER PREVENTION(70,3)|SOLID WASTE SLURRY(61,59)|CONSUME DEAL(49,1)|FOAMING PASTE FILLING(41,3)|PASTE FILLING MASTER BATCH(39,2)|SOLID WASTE(36,94)|MASTER BATCH(36,8)|COAL MINING(36,2)|PASTE FILLER(35,6)|SUPERCRITICAL STABLE(35,3)|DYNAMIC DISASTER(34,2)|FOAM PASTE FILLER(33,7)|LIGHTWEIGHT(33,2)|COMPRESSION RESISTANCE(31,3)|CRUSHING(30,6)|ENERGY ABSORPTION CAPACITY(30,1)|MIXER(26,46)|CARBON DIOXIDE DEAL(26,1)|HEAT PRESERVATION(25,4)|DEFECT(25,1)|MIXING WATER(23,6)|PERFORMING HEAT INSULATION(23,4)|ENERGY ABSORBING PASTE FILLER(22,2)|GANGUE(22,1)|SUPERCRITICAL CARBON DIOXIDE(21,6)|FOAM CORE(18,3)|ENVIRONMENTAL CONDITION(18,2)|RELEASING PRESSURE(18,2)|FOAM PASTE FILLER PRESSURE(17,1)|ENERGY ABSORPTION FUNCTION(16,11)|CONTROLLABLE CELL STRUCTURE(16,2)|CEMENT(15,2)|STIRRING(13,6)|INJECTION VOLUME(13,3)|AIR MIXING(13,2)|FINE PARTICLE(13,1)|RAW MATERIAL(11,14)|CARBON DIOXIDE(11,8)|HEAT INSULATION(11,1)|SOLID WASTE RAW MATERIAL(9,14)|FILLING BODY MASTER BATCH(9,5)|FILLING MATERIAL(9,4)|COAL GANGUE(9,2)|CONTROLLABLE FOAM CELL STRUCTURE(9,2)|CURED PASTE FILLING(9,2)|FOAM PASTE FILLING(9,2)|RAPID PRESSURE RELIEF(9,2)|MILITARY EXPLOSION PREVENTION(9,1)|OVERLYING MINING ROCK(9,1)|PRESSURE RELEASE SPEED(8,1)|CARBON FIXING FUNCTION(7,3)|CONVEYING VALVE(7,3)|PARTICLE SIZE(7,3)|FOAM NUCLEUS(7,2)|INORGANIC SUBSTANCE(7,2)|ATHLETE SOLE SHOCK ABSORPTION(7,1)|COAL EXPLOITATION(7,1)|FOAMING PASTE FILLER SLURRY(7,1)|LOOSE PASTE FILLING(7,1)|MINING PASTE FILLING(7,1)|MULTIDISASTER PREVENTION(7,1)|PREMATURE COAGULATION(7,1)|SLURRY RETURNING BLOCKAGE(7,1)|STRATEGY TRACTION(7,1)|SYNERGISTIC DISASTER PREVENTION(7,1)|PREPARATION EQUIPMENT(6,4)|CARBONIZATION REACTION(6,2)|DELIVERY VALVE(6,2)|POSITIONAL RELATIONSHIP(6,2)|COAL RESOURCE(6,1)|DIFFUSION PERMEATION(6,1)|HARMFUL BYPRODUCT(6,1)|PASTE FILLER MASTER BATCH(6,1)|POROSITY ANALYZER(6,1)|ROCK BURST(6,1)|TURBINE STIRRER(6,1)|PIPELINE(5,3)|DIFFUSIVITY(5,2)|SIGNIFICANCE(5,2)|3D MICROSCOPE(5,1)|CELL MORPHOLOGY(5,1)|CURING MAINTENANCE CHAMBER(5,1)|CURING OXIDATION CHAMBER(5,1)|DYNAMIC ADJUSTMENT PROPORTION(5,1)|FOAM FILLER POROSITY(5,1)|FUNDAMENTAL TRANSITION(5,1)|HIGH ENERGY ABSORPTION(5,1)|MINE ENVIRONMENT(5,1)|MINERALIZATION REACTION(5,1)|SOLIDIFIED FILLER COMPRESSIVE STRENGTH(5,1)|TURBINE STIRRING(5,1)|PRESSURE REACTOR(4,18)|SOLID WASTE FILLING(4,4)|PARTICLE RATIO(4,3)|STIRRING TIME(4,3)|COAL MINE(4,2)|NEGATIVE INFLUENCE(4,2)|PERMEABILITY(4,2)|BASIC MATERIAL(4,1)|BUBBLE CORE(4,1)|CARBON EXPLOITATION(4,1)|COAL DEVELOPMENT(4,1)|COAL SOLID CARBON SLURRY(4,1)|CURED COAL SOLID WASTE(4,1)|CURING CHAMBER(4,1)|DIFFUSION DISSOLUTION REACTION BEHAVIOR(4,1)|FACULTY(4,1)|FLUIDITY(4,1)|FULL PERMEATION REACTION(4,1)|GREEN MINE CONSTRUCTION(4,1)|INJECTION COMPLETION(4,1)|ORDINARY MEANING(4,1)|PRESOLIDIFICATION(4,1)|SAFETY REQUIREMENT(4,1)|SLURRY INJECTION(4,1)|STIRRING DIFFICULTY(4,1)|TEMPERATURE FLUCTUATION INTERFERENCE(4,1)|UNDERGROUND MINE STRESS WAVE(4,1)| (CN119951390)|1. The method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming is characterized by comprising the following steps of:| crushing and grinding the coal-based solid waste raw materials, and stirring and mixing the crushed and ground coal-based solid waste raw materials with mixing water at a speed of less than 60r/min to prepare coal-based solid waste slurry, wherein particles with a particle size of less than 20 mu m account for more than 15% in powder formed by crushing and grinding the coal-based solid waste raw materials; | The prepared coal-based solid waste slurry is injected into a preheated high-temperature high-pressure mixer for stirring, and supercritical CO 2 is continuously injected in the stirring process, wherein the injection volume of the coal-based solid waste slurry is 1/3-1/2 of the volume of the high-temperature high-pressure mixer, so that the supercritical CO 2 fully permeates with the coal-based solid carbon slurry in the high-temperature high-pressure mixer to give enough space to form a uniform cell structure, the temperature of the high-temperature high-pressure mixer is kept above 31 ℃, the pressure is kept above 7.3 MPa, so that the supercritical CO 2 is kept in a supercritical stable state at high temperature and high pressure in the high-temperature high-pressure mixer and fully permeates into the coal-based solid waste slurry to form a mixture of the supercritical CO 2 and the coal-based solid waste slurry; | The method comprises the steps of mixing and stirring supercritical CO 2 and coal-based solid waste slurry mixture at high temperature and high pressure to form foam paste filler master batch, controlling the heat preservation and pressure maintaining time at high temperature and high pressure for 10-30min, then releasing pressure, and controlling the pressure maintaining time to prevent the coal-based solid waste slurry from pre-coagulating, so as to ensure sufficient fluidity of the coal-based solid waste slurry, controlling the pressure release speed to be 2.5MPa/s when the pressure of the foam paste filler master batch is released after Wen Baoya, gradually reducing the pressure in a high-temperature high-pressure mixer to be 0-7.4MPa, controlling the pressure release speed to be 2.5MPa/s, wherein the pressure release speed is not too fast, otherwise, CO 2 in the high-temperature high-pressure mixer generates dry ice, the foaming effect is influenced, and a large amount of paste with a carbon-fixing and energy-absorbing function taking supercritical CO 2 as a foam core is formed, and the stirring process is carried out under high-pressure high-temperature conditions, so that SC-CO 2 has higher diffusivity and permeability, and can rapidly permeate the coal-based solid waste slurry. |2. The method for preparing the paste filler with the carbon fixation and energy absorption functions based on SC-CO 2 foaming according to claim 1, wherein the coal-based solid waste slurry is stirred at a speed of less than 60r/min for 6-10min.|3. The method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming according to claim 1, wherein the speed of mixing and stirring the supercritical CO 2 and coal-based solid waste slurry mixture in a high-temperature and high-pressure mixer is 300-400r/min, and the stirring time is 8-10min.|4. The carbon-fixing energy-absorbing paste filler prepared by the method for preparing the carbon-fixing energy-absorbing paste filler based on SC-CO 2 foaming according to any one of claims 1 to 3. (CN119951390)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of coal mining, in particular to a method for preparing a paste filling body with carbon fixation and energy absorption functions based on SC-CO 2 foaming.|BACKGROUND ART|[0002] Coal plays an important role in guaranteeing the energy safety of China and still faces the fundamental transition from the traditional utilization mode to low-carbon efficient mining. With the increasing severity of global climate change and carbon emission problems, the mining industry is urgent to develop a filling material with a carbon fixing function to reduce carbon dioxide emission and promote green mine construction. The practical problem of large-scale goaf formation and massive CO 2 emission in the coal exploitation and consumption process is forced to be overcome.|[0003] The preparation of the traditional filling material with the carbon fixing function needs to consume a great deal of time and resources, a great deal of carbon dioxide is usually generated in the manufacturing process, the traditional filling material mainly uses cement and gangue or waste stone as basic materials, the density is high, the energy absorbing capacity is poor, and the requirements of high compression resistance and high energy absorption required by the prevention and control of mining dynamic disasters are difficult to meet. The existing paste filling material has obvious defects in the aspects of light weight, heat insulation and the like, and is difficult to adapt to the actual requirements of mine dynamic environment and dynamic disaster prevention and control.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to overcome the problems in the prior art, and provides the paste filling body prepared by the method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming, which has low density, high strength, good heat insulation performance and controllable cell structure, can be used for a long time under various extreme environmental conditions, and can better adapt to the actual requirements of mine dynamic environment and dynamic disaster prevention and control.|[0005] The invention relates to a method for preparing a paste filling body with carbon fixation and energy absorption functions based on SC-CO 2 foaming, which comprises the following steps of crushing and grinding coal-based solid waste raw materials, stirring and mixing the crushed and ground coal-based solid waste raw materials with mixing water at a speed of less than 60r/min to prepare coal-based solid waste slurry;|[0006] Injecting the prepared coal-based solid waste slurry into a preheated high-temperature high-pressure mixer for stirring, and continuously injecting supercritical CO 2 in the stirring process, wherein the temperature of the high-temperature high-pressure mixer is kept above 31 ℃, and the pressure is kept above 7.3MPa, so that the supercritical CO 2 is kept in a supercritical stable state in the high-temperature high-pressure mixer, and fully permeates into the coal-based solid waste slurry to form a mixture of the supercritical CO 2 and the coal-based solid waste slurry; |[0007] Mixing and stirring the supercritical CO 2 and the coal-based solid waste slurry mixture at high temperature and high pressure to form a foam paste filling body master batch, controlling the heat preservation and pressure maintaining time of the foam paste filling body master batch at high temperature and high pressure for 10-30min, and then releasing pressure, wherein in the pressure releasing process, the supercritical CO 2 is converted into a gas state from the supercritical state, and bubbles are gradually formed in the coal-based solid waste slurry to form a large amount of paste filling bodies with carbon fixation and energy absorption functions, wherein the carbon fixation and energy absorption functions take supercritical CO 2 as bubble cores. |[0008] Preferably, the injection volume of the coal-based solid waste slurry is 1/3-1/2 of the volume of the high-temperature high-pressure mixer.|[0009] Preferably, the coal-based solid waste slurry is stirred at a speed of less than 60r/min for 6-10min.|[0010] Preferably, the speed of mixing and stirring the supercritical CO 2 and coal-based solid waste slurry mixture in the high-temperature high-pressure mixer is 300-400r/min, and the stirring time is 8-10min.|[0011] Preferably, when the foam paste filler master batch is depressurized after Wen Baoya, the pressure relief speed is controlled to be 2.5MPa/s, and the pressure in the high-temperature high-pressure mixer is gradually reduced to 0-7.4MPa.|[0012] Preferably, the powder formed by crushing and grinding the coal-based solid waste raw material has a particle size of less than 20 μm and a particle ratio of 15% or more.|[0013] The invention also provides a method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming, and the paste filling body with the carbon fixation and energy absorption functions is prepared.|[0014] Compared with the prior art, the method has the beneficial effects that the coal-based solid waste raw material is crushed and ground into fine particles with the particle size smaller than 20 mu m, meanwhile, in the process of preparing the coal-based solid waste slurry, air mixing can be avoided by adopting a low-speed stirring mode, meanwhile, when the prepared coal-based solid waste slurry is injected with supercritical CO 2, the supercritical CO 2 is injected while stirring at high temperature and high pressure, the supercritical CO 2 can be fully permeated into the coal-based solid waste slurry to form a mixture of the supercritical CO 2 and the coal-based solid waste slurry, and meanwhile, the mixture of the supercritical CO 2 and the coal-based solid waste slurry is mixed and stirred at high temperature and high pressure, so that the problems that the coal-based solid waste slurry is compacted, the pore forming is difficult and a foaming paste filling body cannot be formed due to high pressure are avoided when the supercritical carbon dioxide is injected into the coal-based solid waste slurry. The paste filling body with the carbon fixation and energy absorption functions prepared by the preparation method disclosed by the invention has the advantages of excellent performance, low density, light weight, high compression resistance, good heat insulation performance and controllable cell structure, can be used for a long time under various extreme environmental conditions, and is suitable for actual requirements of mine dynamic environment and dynamic disaster prevention and control.|[0015] The mineral substances in the slurry of the coal-based solid waste foaming paste filler are carbonated and hardened due to the dissolution of CO 2 and the reaction with water, so that the filler has better strength and durability, the number of pores with the diameter of more than 1000 nanometers is reduced due to the dissolution and chemical reaction effects of CO 2 bubbles, the compressive strength of the slurry of the coal-based solid waste foaming paste filler is enhanced, and the negative influence of the increase of the porosity on the slurry of the coal-based solid waste CO 2 foaming paste filler is furthest reduced.|[0016] Compared with the traditional chemical foaming agent, the supercritical carbon dioxide serving as the physical foaming agent is nontoxic, is environmentally friendly in production and low in cost, has high diffusivity and strong permeability, does not generate harmful byproducts when being subjected to carbonization reaction with coal-based solid waste slurry, and has obviously higher foaming efficiency than the traditional chemical foaming agent. And the space can be filled according to the dynamic adjustment proportion of the solid waste yield of the coal base under the specification of the space to be filled (goaf), so that materials are saved, CO 2 can be stored in the foam holes, dynamic and static loads applied by the overlying mining rock body are borne by the internal pressure, and meanwhile, the stress wave propagation generated by the fracture of the overlying rock layer is absorbed and dissipated, and finally, the whole process of coal development and utilization of 'near-zero ecological damage, near-zero rock burst and carbon exploitation' is realized. The invention endows the mine filling material with the requirements of light weight, high compression resistance, energy absorption, carbon fixation, low cost and the like, ensures the stable supply of energy, promotes the development of green low carbon of coal resources, solves the practical difficult problem of safe, efficient, green and low carbon mining of coal mines, and has important theoretical significance and practical requirements.|DRAWINGS DESCRIPTION|[0017] Fig. 1 is a schematic diagram of a paste filling body with carbon fixation and energy absorption functions according to an embodiment of the invention.|[0018] Fig. 2 is a schematic diagram of a paste filling device with carbon fixation and energy absorption functions according to an embodiment of the invention.|[0019] FIG. 3 is a schematic diagram of a paste filling device with carbon fixation and energy absorption functions, which is arranged in an incubator according to an embodiment of the invention.|INVENTION MODE|Detailed Description|[0020] For the purpose of making the objects, technical solutions and advantages of the embodiments of the present disclosure more apparent, the technical solutions of the embodiments of the present disclosure will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present disclosure. It will be apparent that the described embodiments are some, but not all, of the embodiments of the present disclosure. All other embodiments, which can be made by one of ordinary skill in the art without the need for inventive faculty, are within the scope of the present disclosure, based on the described embodiments of the present disclosure.|[0021] Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this disclosure belongs. The terms "first," "second," and the like, as used in this disclosure, do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. The word "comprising" or "comprises", and the like, is intended to mean that elements or items that are present in front of "comprising" or "comprising" are included in the word "comprising" or "comprising", and equivalents thereof, without excluding other elements or items. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", etc. are used merely to indicate relative positional relationships, and when the absolute position of the object to be described is changed, the relative positional relationships may be changed accordingly.|[0022] In the field of mine filling, the filling body with uniform and fine cell structures has outstanding effect in the aspect of energy absorption performance, the requirement on the aspect of underground mine stress wave absorption is larger, the cell structures in the filling material can deform, impact energy can be absorbed and dissipated, the excellent gradient energy absorption performance is shown, and the filling body has important significance for preventing and controlling chain mine dynamic disasters such as rock burst, gas explosion and the like.|[0023] With the improvement of environmental protection and mine safety requirements, under the traction of a strategy of 'double-carbon driven high-quality development', a low-carbon foaming technology taking supercritical CO 2 as a foaming agent is accepted in the field of polymer foaming, the excellent carbon fixation and energy absorption effects are remarkable in energy absorption and shock absorption, military explosion prevention or athlete sole shock absorption is represented remarkably, in the field of mine filling, no precedent of using supercritical carbon dioxide as a coal-based solid waste foaming agent exists at present, and the invention is used and tried for the first time in the field of mining paste filling. The high-temperature and high-pressure mixer adopted in the invention has a stirring function, so that SC-CO 2 has higher diffusivity and permeability, can rapidly permeate into coal-based solid waste slurry, and fully ensures the permeation reaction of supercritical CO 2 and the coal-based solid waste slurry.|[0024] The method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming provided by the embodiment comprises the following steps:|[0025] Crushing and grinding the coal-based solid waste raw material to powder with particle diameter smaller than 20 mu m and particle ratio larger than 15%, and stirring and mixing the powder and mixing water at a speed smaller than 60r/min to prepare the coal-based solid waste slurry. The coal-based solid waste raw materials in the embodiment are coal-based solid waste raw materials such as coal gangue and fly ash. |[0026] Injecting the prepared coal-based solid waste slurry into a preheated high-temperature high-pressure mixer for stirring, and continuously injecting supercritical CO 2 in the stirring process until the pressure of the high-temperature high-pressure mixer is the same as that of a CO 2 gas supply device, wherein the supercritical CO 2 is obtained by pressurizing a CO 2 gas supply device through a high-pressure pump and is stored in a high-temperature high-pressure reactor 4;|[0027] The temperature of the high-temperature high-pressure mixer 10 is kept above 31 ℃, the pressure is kept above 7.3MPa, so that the supercritical CO 2 is kept in a supercritical stable state in the high-temperature high-pressure mixer 10, and fully permeates into the coal-based solid waste slurry to form a mixture of the supercritical CO 2 and the coal-based solid waste slurry; |[0028] The supercritical CO 2 and coal-based solid waste slurry mixture are mixed and stirred in the high-temperature high-pressure mixer 10 to form a foam paste filler master batch, the supercritical CO 2 can be maintained in a supercritical state at the high temperature and the high pressure of the high-temperature high-pressure mixer 10, and meanwhile, the problem that the coal-based solid waste slurry is compacted, the pore forming is difficult and the foam paste filler cannot be formed due to the fact that the coal-based solid waste slurry is subjected to high pressure when supercritical carbon dioxide is injected into the coal-based solid waste slurry is avoided through a stirring mode. The high temperature and high pressure in this example means that the temperature of the high temperature and high pressure mixer is maintained at 31 ℃ or higher and the pressure is maintained at 7.3MPa or higher. |[0029] In the embodiment, the foam paste filler master batch is selected to be subjected to pressure relief after being subjected to heat preservation and pressure maintaining for 10-30min in the high-temperature high-pressure mixer 10, and the foam paste filler master batch is subjected to pressure relief after being subjected to heat preservation and pressure maintaining for 10-30min in the high-temperature high-pressure mixer 10, because a certain time is required for carbonization reaction between supercritical CO 2 and the coal-based solid waste slurry mixture to form a stable cell structure, meanwhile, under the high-temperature high-pressure condition, supercritical CO 2 can be uniformly diffused in the coal-based solid waste slurry mixture, a foundation is provided for forming uniform bubbles in the subsequent pressure relief process, CO 2 in the mixer is converted from supercritical to gaseous state in the pressure relief process, bubbles are gradually formed in the coal-based solid waste slurry, and a large amount of coal-based solid waste foaming paste filler slurry taking supercritical CO 2 as a foam core is formed, so that foaming of the paste filler master batch is realized.|[0030] Fig. 1 illustrates a preparation flow chart of a paste filling body with carbon fixation and energy absorption functions in the embodiment, the paste filling body is prepared by crushing and grinding coal-based solid waste raw materials and mixing with mixing water at a speed of less than 60r/min, CO 2 in a supercritical state is continuously injected into a turbine stirrer until the supercritical CO 2 is the same as the set pressure, the supercritical CO 2 and the coal-based solid waste paste are formed, the supercritical CO 2 and the coal-based solid waste paste are fully mixed through turbine stirring, a foam paste filling body master batch is formed, namely paste filling body master batch in the embodiment is subjected to rapid pressure relief after heat preservation and pressure maintaining for 10-30min in the high-temperature high-pressure mixer, a large amount of foam paste filling body master batch of the coal-based solid waste foam paste taking supercritical CO 2 as a foam nucleus is formed, the filling body has a low-density, good heat insulation performance and a controllable foam cell structure, the active and multi-disaster prevention and control effect of a coal mine can be realized from a deep power factor control and a power factor, and a synergistic disaster prevention effect can be realized.|[0031] In one embodiment of the present invention, the coal-based solid waste slurry injection volume is 1/3-1/2 of the volume of the high temperature high pressure mixer to ensure that supercritical CO 2 is sufficiently permeated with the coal-based solid carbon slurry in the high temperature high pressure mixer 10 to give enough room to form a uniform cell structure. If the ratio of the coal-based solid waste slurry in the high temperature and high pressure mixer 10 is too large, the diffusion permeation rate of CO 2 may be affected, affecting the foaming result. Meanwhile, the excessive pressure in the high-temperature high-pressure mixer 10 is avoided, and the safety of equipment is prevented from being influenced. And the range can avoid slurry returning blockage caused by filling the high-temperature high-pressure mixer with the coal-based solid waste slurry, stirring difficulty caused by uneven CO 2 distribution and premature coagulation of the coal-based solid waste slurry.|[0032] In another preferred embodiment, when the coal-based solid waste slurry is prepared, stirring is carried out at a speed of less than 60r/min for 6-10min, and stirring at a speed of less than 60r/min in the time range can avoid air mixing, so that the subsequent full permeation reaction with supercritical CO 2 is facilitated.|[0033] In another preferred embodiment, the supercritical CO 2 and coal-based solid waste slurry mixture is mixed and stirred at a speed of 300-400r/min for a period of 8-10min.|[0034] When the foam paste filling body master batch is depressurized after Wen Baoya, the pressure relief speed is controlled to be 2.5MPa/s, and the pressure in the high-temperature high-pressure mixer is gradually reduced to 0-7.4MPa.|[0035] The embodiment also provides the coal-based solid waste CO 2 foaming paste filling body prepared by the method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming.|[0036] The preparation process described above is described in further detail below by way of specific examples.|[0037] When the preparation method of the embodiment is implemented, corresponding preparation equipment needs to be built, the preparation equipment can be equipment meeting the use condition in the prior art or equipment built according to the embodiment, as shown in fig. 2, the preparation equipment built according to the embodiment comprises a CO 2 air supply device 1, a high-temperature high-pressure reactor 4, a high-temperature high-pressure mixer 10, a curing oxidation chamber 12 and a constant-temperature box 13 which are sequentially connected through pipelines, wherein the tops of the CO 2 air supply device 1 and the high-temperature high-pressure reactor 4 are provided with a pressure gauge 2, the pipelines between the CO 2 air supply device 1 and the high-temperature high-pressure reactor 4 and the pipelines between the high-temperature high-pressure reactor 4 and the high-temperature high-pressure mixer 10 are respectively provided with a conveying valve 3, the high-temperature high-pressure mixer 10 is provided with a pressure sensor 6 and a temperature sensor 7 for detecting the internal pressure and the temperature of the high-temperature high-pressure mixer 10, the high-temperature high-pressure mixer 10 is further provided with a slurry feed port 9 and a pressure release valve 8, and the high-temperature high-pressure mixer 10 is internally provided with a stirring device 11 along the vertical direction.|[0038] As shown in FIG. 3, the high-temperature high-pressure reactor 4, the high-pressure pump 5, the pressure sensor 6, the temperature sensor 7, the pressure release valve 8, the slurry feed port 9, the high-temperature high-pressure mixer 10, the stirring device 11 and the curing maintenance chamber 12 are all arranged in the constant temperature box 13, so that all equipment in the experiment can be ensured to operate within a set temperature range, the interference of external temperature fluctuation on the experimental result can be avoided, and meanwhile, the sensor is matched for monitoring the temperature and the pressure change in the experiment in real time, so that a stable working environment is provided for the high-temperature high-pressure mixer 10 and the stirring device 11, the slurry is ensured to be fully mixed at an ideal temperature, and experimental errors caused by uneven temperature can be avoided. After the preparation equipment is built, crushing coal-based solid waste raw materials such as coal gangue and fly ash, grinding the crushed coal-based solid waste raw materials into powder with particle diameter of less than 20 mu m and particle ratio of more than 15%, stirring and mixing the powder with mixing water at a low speed of 60r/min for 6-10min, and obtaining coal-based solid waste slurry after stirring by adopting the low-speed stirring mode, wherein the prepared coal-based solid waste slurry waits to be injected into a high-temperature and high-pressure mixer;|[0039] The high temperature and high pressure mixer 10 is preheated to reduce the waiting time of the coal-based solid waste slurry injected later in the high temperature and high pressure mixer. |[0040] The high-temperature high-pressure reactor 4 is preheated to prevent pressure shock caused by temperature shock, the pressure and the temperature in the high-temperature high-pressure reactor 4 are regulated to ensure that the high temperature and the high pressure in the high-temperature high-pressure reactor 4 are kept in a high-temperature 31 ℃ range and the high pressure is kept in a 7.3MPa range, so that the pressure and the temperature in the process of converting gaseous CO 2 into supercritical CO 2 in the high-temperature high-pressure reactor 4 are cooperatively regulated;|[0041] the delivery valve between the CO 2 gas supply device 1 and the high-temperature high-pressure reactor 4 is opened, CO 2 is continuously injected into the high-temperature high-pressure reactor 4 through the pressure difference between the CO 2 gas supply device 1 and the high-temperature high-pressure reactor 4, the high-temperature high-pressure reactor 4 is in a vacuum state at this time, about-0.02 MPa, and the delivery valve is closed until the pressure in the high-temperature high-pressure reactor 4 is approximately the same as the pressure in the CO 2 gas supply device 1. |[0042] And (3) carrying out heat preservation and pressure maintaining on the gaseous CO 2 injected into the high-temperature high-pressure reactor 4 in the pressure temperature range (the high temperature is 31 ℃ and the high pressure is kept in the range of 7.3 MPa) until the gaseous CO 2 in the high-temperature high-pressure reactor 4 reaches the state of phase change and is converted into supercritical carbon dioxide, namely SC-CO 2.|[0043] Injecting the prepared coal-based solid waste slurry into a container through a slurry feed inlet above the high-temperature high-pressure mixer 10, completing injection when the injection volume is 1/3 of the volume of the high-temperature high-pressure mixer 10, and closing the coal-based solid waste slurry feed inlet to inject the coal-based solid waste slurry, wherein the inside of the high-temperature high-pressure mixer 10 is in a vacuum state of about-0.02 MPa;|[0044] In this embodiment, a stirring device 11 is vertically arranged inside the high-temperature and high-pressure mixer 10, the stirring device 11 in this embodiment is preferably a turbine type stirrer, and after the injection of the coal-based solid waste slurry is completed and the feeding port of the coal-based solid waste slurry is closed, a spiral stirring rod in the high-temperature and high-pressure mixer 10 is started to stir the injected coal-based solid waste slurry; |[0045] In the stirring process of the coal-based solid waste slurry, a conveying valve 3 between a high-temperature high-pressure reactor 4 and a high-temperature high-pressure mixer 10 is opened, a high-pressure pump is started, supercritical carbon dioxide, namely SC-CO 2, is continuously pumped into the high-temperature high-pressure mixer 10 at constant temperature and constant pressure in the stirring process, supercritical CO 2 is pumped into the mixer while stirring, and the conveying valve 3 is closed after the pressure of a CO 2 air supply device 1 is the same as that of the high-temperature high-pressure mixer 10. In the embodiment, CO 2 is continuously injected into the coal-based solid waste slurry in the stirring process, so that the compressive strength of the solidified filler can be improved; |[0046] Further, by adjusting and observing the pressure sensor 6 and the temperature sensor 7 above the high-temperature high-pressure mixer 10, the high-temperature high-pressure mixer 10 is kept in a heat preservation and pressure maintaining state, namely in a temperature 31 ℃ range, and supercritical CO 2 is fully permeated into the coal-based solid waste slurry within a pressure 7.3MPa range, so that a mixture of the supercritical CO 2 and the coal-based solid waste slurry is formed; |[0047] Then under the conditions of high pressure and high temperature, continuously stirring and mixing the mixture in the high temperature and high pressure mixer 10 by a spiral stirring rod, wherein the stirring speed is 300-400r/min, the stirring time is 8-10min, and the foam paste filling master batch is formed; |[0048] The heat preservation and pressure maintaining time of the foam paste filling body master batch formed after stirring is controlled to be 10min in the high-temperature high-pressure mixer 10, the pre-solidification of the coal-based solid waste slurry is avoided by controlling the pressure maintaining time, the sufficient fluidity of the coal-based solid waste slurry is ensured, a pressure relief valve 8 above the high-temperature high-pressure mixer 10 is opened, the pressure relief speed is controlled to be 2.5MPa/s, the pressure relief speed is not too fast, otherwise, the CO 2 in the high-temperature high-pressure mixer 10 generates dry ice to influence the foaming effect, the pressure in the high-temperature high-pressure mixer 10 is gradually reduced to 0MPa, at the moment, the SC-CO 2 in the high-temperature high-pressure mixer 10 is in a reduced pressure state condition, the CO 2 with larger density is desolventized, the CO 2 is converted into a gaseous state by supercritical, the CO 2 in the solution is released, the gas volume is rapidly expanded, a large amount of bubbles are formed, and the foaming of the paste filling body master batch is realized, and a large amount of the coal-based solid waste foaming filling body slurry taking supercritical CO 2 as a foam nucleus is formed. |[0049] The mineral substances in the slurry of the coal-based solid waste foaming paste filler are carbonated and hardened due to the dissolution of CO 2 and the reaction with water, so that the filler has better strength and durability, the number of pores with the diameter of more than 1000 nanometers is reduced due to the dissolution and chemical reaction effects of CO 2 bubbles, the compressive strength of the slurry of the coal-based solid waste foaming paste filler is enhanced, and the negative influence of the increase of the porosity on the slurry of the coal-based solid waste CO 2 foaming paste filler is reduced to the greatest extent;|[0050] And (3) injecting the slurry of the coal-based solid waste filling body in the high-temperature and high-pressure mixer into a curing chamber 12, and curing for a time to form the cured coal-based solid waste CO 2 foaming paste filling body. The original loose paste filling body is changed into a honeycomb-shaped (CO 2 cell structure) filling body with high strength, high elasticity and energy absorption property through the foaming process. |[0051] The development of supercritical CO 2 foam-filler porosity is affected by the diffusion-dissolution-reaction behavior of CO 2 in supercritical CO 2 -filler systems.|[0052] In the embodiment, density and porosity effect tests are carried out on the cured paste filling body with the carbon fixation and energy absorption functions, the cell morphology of the paste filling body with the carbon fixation and energy absorption functions is observed by a 3D microscope, and the test is carried out by a BSD-TD-K full-automatic true density and porosity analyzer, so that the density of the paste filling body with the carbon fixation and energy absorption functions is 35% -50% lower than that of the traditional cement-based filling material, and the porosity is 45% -80%, and the paste filling body with the carbon fixation and energy absorption functions is obviously superior to that of the traditional cementing filling body.|[0053] The energy absorption performance test verification is carried out on the cured CO 2 foaming coal-based solid waste filling body in the embodiment, the mine environment is simulated, the energy absorption characteristic of the CO 2 foaming coal-based solid waste filling body is tested by adopting a pressure sensor, and the result shows that the paste filling body with the carbon fixation and energy absorption functions prepared in the embodiment can absorb 50% -70% of energy of shock waves, and compared with the traditional filling body (such as cement and gypsum-based filling materials), the energy absorption effect is improved by 30% -50%.|[0054] In the embodiment, the carbon fixing function effect test verification is carried out on the cured paste filling body with the carbon fixing and energy absorbing functions, the X-ray diffraction (XRD) technology is adopted to test the paste filling body with the carbon fixing and energy absorbing functions, the mineralization reaction of CO and minerals in coal-based solid waste slurry is verified, the carbon fixing rate of the prepared CO 2 foaming coal-based solid waste filling body in the foaming process is 6-11%, and the carbon storage amount of cells is 1-2kg.|[0055] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. (CN119951390)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of coal mining, in particular to a method for preparing a paste filling body with carbon fixation and energy absorption functions based on SC-CO 2 foaming.|BACKGROUND ART|[0002] Coal plays an important role in guaranteeing the energy safety of China and still faces the fundamental transition from the traditional utilization mode to low-carbon efficient mining. With the increasing severity of global climate change and carbon emission problems, the mining industry is urgent to develop a filling material with a carbon fixing function to reduce carbon dioxide emission and promote green mine construction. The practical problem of large-scale goaf formation and massive CO 2 emission in the coal exploitation and consumption process is forced to be overcome.|[0003] The preparation of the traditional filling material with the carbon fixing function needs to consume a great deal of time and resources, a great deal of carbon dioxide is usually generated in the manufacturing process, the traditional filling material mainly uses cement and gangue or waste stone as basic materials, the density is high, the energy absorbing capacity is poor, and the requirements of high compression resistance and high energy absorption required by the prevention and control of mining dynamic disasters are difficult to meet. The existing paste filling material has obvious defects in the aspects of light weight, heat insulation and the like, and is difficult to adapt to the actual requirements of mine dynamic environment and dynamic disaster prevention and control.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to overcome the problems in the prior art, and provides the paste filling body prepared by the method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming, which has low density, high strength, good heat insulation performance and controllable cell structure, can be used for a long time under various extreme environmental conditions, and can better adapt to the actual requirements of mine dynamic environment and dynamic disaster prevention and control.|[0005] The invention relates to a method for preparing a paste filling body with carbon fixation and energy absorption functions based on SC-CO 2 foaming, which comprises the following steps of crushing and grinding coal-based solid waste raw materials, stirring and mixing the crushed and ground coal-based solid waste raw materials with mixing water at a speed of less than 60r/min to prepare coal-based solid waste slurry;|[0006] Injecting the prepared coal-based solid waste slurry into a preheated high-temperature high-pressure mixer for stirring, and continuously injecting supercritical CO 2 in the stirring process, wherein the temperature of the high-temperature high-pressure mixer is kept above 31 ℃, and the pressure is kept above 7.3MPa, so that the supercritical CO 2 is kept in a supercritical stable state in the high-temperature high-pressure mixer, and fully permeates into the coal-based solid waste slurry to form a mixture of the supercritical CO 2 and the coal-based solid waste slurry; |[0007] Mixing and stirring the supercritical CO 2 and the coal-based solid waste slurry mixture at high temperature and high pressure to form a foam paste filling body master batch, controlling the heat preservation and pressure maintaining time of the foam paste filling body master batch at high temperature and high pressure for 10-30min, and then releasing pressure, wherein in the pressure releasing process, the supercritical CO 2 is converted into a gas state from the supercritical state, and bubbles are gradually formed in the coal-based solid waste slurry to form a large amount of paste filling bodies with carbon fixation and energy absorption functions, wherein the carbon fixation and energy absorption functions take supercritical CO 2 as bubble cores. |[0008] Preferably, the injection volume of the coal-based solid waste slurry is 1/3-1/2 of the volume of the high-temperature high-pressure mixer.|[0009] Preferably, the coal-based solid waste slurry is stirred at a speed of less than 60r/min for 6-10min.|[0010] Preferably, the speed of mixing and stirring the supercritical CO 2 and coal-based solid waste slurry mixture in the high-temperature high-pressure mixer is 300-400r/min, and the stirring time is 8-10min.|[0011] Preferably, when the foam paste filler master batch is depressurized after Wen Baoya, the pressure relief speed is controlled to be 2.5MPa/s, and the pressure in the high-temperature high-pressure mixer is gradually reduced to 0-7.4MPa.|[0012] Preferably, the powder formed by crushing and grinding the coal-based solid waste raw material has a particle size of less than 20 μm and a particle ratio of 15% or more.|[0013] The invention also provides a method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming, and the paste filling body with the carbon fixation and energy absorption functions is prepared.|[0014] Compared with the prior art, the method has the beneficial effects that the coal-based solid waste raw material is crushed and ground into fine particles with the particle size smaller than 20 mu m, meanwhile, in the process of preparing the coal-based solid waste slurry, air mixing can be avoided by adopting a low-speed stirring mode, meanwhile, when the prepared coal-based solid waste slurry is injected with supercritical CO 2, the supercritical CO 2 is injected while stirring at high temperature and high pressure, the supercritical CO 2 can be fully permeated into the coal-based solid waste slurry to form a mixture of the supercritical CO 2 and the coal-based solid waste slurry, and meanwhile, the mixture of the supercritical CO 2 and the coal-based solid waste slurry is mixed and stirred at high temperature and high pressure, so that the problems that the coal-based solid waste slurry is compacted, the pore forming is difficult and a foaming paste filling body cannot be formed due to high pressure are avoided when the supercritical carbon dioxide is injected into the coal-based solid waste slurry. The paste filling body with the carbon fixation and energy absorption functions prepared by the preparation method disclosed by the invention has the advantages of excellent performance, low density, light weight, high compression resistance, good heat insulation performance and controllable cell structure, can be used for a long time under various extreme environmental conditions, and is suitable for actual requirements of mine dynamic environment and dynamic disaster prevention and control.|[0015] The mineral substances in the slurry of the coal-based solid waste foaming paste filler are carbonated and hardened due to the dissolution of CO 2 and the reaction with water, so that the filler has better strength and durability, the number of pores with the diameter of more than 1000 nanometers is reduced due to the dissolution and chemical reaction effects of CO 2 bubbles, the compressive strength of the slurry of the coal-based solid waste foaming paste filler is enhanced, and the negative influence of the increase of the porosity on the slurry of the coal-based solid waste CO 2 foaming paste filler is furthest reduced.|[0016] Compared with the traditional chemical foaming agent, the supercritical carbon dioxide serving as the physical foaming agent is nontoxic, is environmentally friendly in production and low in cost, has high diffusivity and strong permeability, does not generate harmful byproducts when being subjected to carbonization reaction with coal-based solid waste slurry, and has obviously higher foaming efficiency than the traditional chemical foaming agent. And the space can be filled according to the dynamic adjustment proportion of the solid waste yield of the coal base under the specification of the space to be filled (goaf), so that materials are saved, CO 2 can be stored in the foam holes, dynamic and static loads applied by the overlying mining rock body are borne by the internal pressure, and meanwhile, the stress wave propagation generated by the fracture of the overlying rock layer is absorbed and dissipated, and finally, the whole process of coal development and utilization of 'near-zero ecological damage, near-zero rock burst and carbon exploitation' is realized. The invention endows the mine filling material with the requirements of light weight, high compression resistance, energy absorption, carbon fixation, low cost and the like, ensures the stable supply of energy, promotes the development of green low carbon of coal resources, solves the practical difficult problem of safe, efficient, green and low carbon mining of coal mines, and has important theoretical significance and practical requirements.|DRAWINGS DESCRIPTION|[0017] Fig. 1 is a schematic diagram of a paste filling body with carbon fixation and energy absorption functions according to an embodiment of the invention.|[0018] Fig. 2 is a schematic diagram of a paste filling device with carbon fixation and energy absorption functions according to an embodiment of the invention.|[0019] FIG. 3 is a schematic diagram of a paste filling device with carbon fixation and energy absorption functions, which is arranged in an incubator according to an embodiment of the invention.|INVENTION MODE|Detailed Description|[0020] For the purpose of making the objects, technical solutions and advantages of the embodiments of the present disclosure more apparent, the technical solutions of the embodiments of the present disclosure will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present disclosure. It will be apparent that the described embodiments are some, but not all, of the embodiments of the present disclosure. All other embodiments, which can be made by one of ordinary skill in the art without the need for inventive faculty, are within the scope of the present disclosure, based on the described embodiments of the present disclosure.|[0021] Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this disclosure belongs. The terms "first," "second," and the like, as used in this disclosure, do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. The word "comprising" or "comprises", and the like, is intended to mean that elements or items that are present in front of "comprising" or "comprising" are included in the word "comprising" or "comprising", and equivalents thereof, without excluding other elements or items. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", etc. are used merely to indicate relative positional relationships, and when the absolute position of the object to be described is changed, the relative positional relationships may be changed accordingly.|[0022] In the field of mine filling, the filling body with uniform and fine cell structures has outstanding effect in the aspect of energy absorption performance, the requirement on the aspect of underground mine stress wave absorption is larger, the cell structures in the filling material can deform, impact energy can be absorbed and dissipated, the excellent gradient energy absorption performance is shown, and the filling body has important significance for preventing and controlling chain mine dynamic disasters such as rock burst, gas explosion and the like.|[0023] With the improvement of environmental protection and mine safety requirements, under the traction of a strategy of 'double-carbon driven high-quality development', a low-carbon foaming technology taking supercritical CO 2 as a foaming agent is accepted in the field of polymer foaming, the excellent carbon fixation and energy absorption effects are remarkable in energy absorption and shock absorption, military explosion prevention or athlete sole shock absorption is represented remarkably, in the field of mine filling, no precedent of using supercritical carbon dioxide as a coal-based solid waste foaming agent exists at present, and the invention is used and tried for the first time in the field of mining paste filling. The high-temperature and high-pressure mixer adopted in the invention has a stirring function, so that SC-CO 2 has higher diffusivity and permeability, can rapidly permeate into coal-based solid waste slurry, and fully ensures the permeation reaction of supercritical CO 2 and the coal-based solid waste slurry.|[0024] The method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming provided by the embodiment comprises the following steps:|[0025] Crushing and grinding the coal-based solid waste raw material to powder with particle diameter smaller than 20 mu m and particle ratio larger than 15%, and stirring and mixing the powder and mixing water at a speed smaller than 60r/min to prepare the coal-based solid waste slurry. The coal-based solid waste raw materials in the embodiment are coal-based solid waste raw materials such as coal gangue and fly ash. |[0026] Injecting the prepared coal-based solid waste slurry into a preheated high-temperature high-pressure mixer for stirring, and continuously injecting supercritical CO 2 in the stirring process until the pressure of the high-temperature high-pressure mixer is the same as that of a CO 2 gas supply device, wherein the supercritical CO 2 is obtained by pressurizing a CO 2 gas supply device through a high-pressure pump and is stored in a high-temperature high-pressure reactor 4;|[0027] The temperature of the high-temperature high-pressure mixer 10 is kept above 31 ℃, the pressure is kept above 7.3MPa, so that the supercritical CO 2 is kept in a supercritical stable state in the high-temperature high-pressure mixer 10, and fully permeates into the coal-based solid waste slurry to form a mixture of the supercritical CO 2 and the coal-based solid waste slurry; |[0028] The supercritical CO 2 and coal-based solid waste slurry mixture are mixed and stirred in the high-temperature high-pressure mixer 10 to form a foam paste filler master batch, the supercritical CO 2 can be maintained in a supercritical state at the high temperature and the high pressure of the high-temperature high-pressure mixer 10, and meanwhile, the problem that the coal-based solid waste slurry is compacted, the pore forming is difficult and the foam paste filler cannot be formed due to the fact that the coal-based solid waste slurry is subjected to high pressure when supercritical carbon dioxide is injected into the coal-based solid waste slurry is avoided through a stirring mode. The high temperature and high pressure in this example means that the temperature of the high temperature and high pressure mixer is maintained at 31 ℃ or higher and the pressure is maintained at 7.3MPa or higher. |[0029] In the embodiment, the foam paste filler master batch is selected to be subjected to pressure relief after being subjected to heat preservation and pressure maintaining for 10-30min in the high-temperature high-pressure mixer 10, and the foam paste filler master batch is subjected to pressure relief after being subjected to heat preservation and pressure maintaining for 10-30min in the high-temperature high-pressure mixer 10, because a certain time is required for carbonization reaction between supercritical CO 2 and the coal-based solid waste slurry mixture to form a stable cell structure, meanwhile, under the high-temperature high-pressure condition, supercritical CO 2 can be uniformly diffused in the coal-based solid waste slurry mixture, a foundation is provided for forming uniform bubbles in the subsequent pressure relief process, CO 2 in the mixer is converted from supercritical to gaseous state in the pressure relief process, bubbles are gradually formed in the coal-based solid waste slurry, and a large amount of coal-based solid waste foaming paste filler slurry taking supercritical CO 2 as a foam core is formed, so that foaming of the paste filler master batch is realized.|[0030] Fig. 1 illustrates a preparation flow chart of a paste filling body with carbon fixation and energy absorption functions in the embodiment, the paste filling body is prepared by crushing and grinding coal-based solid waste raw materials and mixing with mixing water at a speed of less than 60r/min, CO 2 in a supercritical state is continuously injected into a turbine stirrer until the supercritical CO 2 is the same as the set pressure, the supercritical CO 2 and the coal-based solid waste paste are formed, the supercritical CO 2 and the coal-based solid waste paste are fully mixed through turbine stirring, a foam paste filling body master batch is formed, namely paste filling body master batch in the embodiment is subjected to rapid pressure relief after heat preservation and pressure maintaining for 10-30min in the high-temperature high-pressure mixer, a large amount of foam paste filling body master batch of the coal-based solid waste foam paste taking supercritical CO 2 as a foam nucleus is formed, the filling body has a low-density, good heat insulation performance and a controllable foam cell structure, the active and multi-disaster prevention and control effect of a coal mine can be realized from a deep power factor control and a power factor, and a synergistic disaster prevention effect can be realized.|[0031] In one embodiment of the present invention, the coal-based solid waste slurry injection volume is 1/3-1/2 of the volume of the high temperature high pressure mixer to ensure that supercritical CO 2 is sufficiently permeated with the coal-based solid carbon slurry in the high temperature high pressure mixer 10 to give enough room to form a uniform cell structure. If the ratio of the coal-based solid waste slurry in the high temperature and high pressure mixer 10 is too large, the diffusion permeation rate of CO 2 may be affected, affecting the foaming result. Meanwhile, the excessive pressure in the high-temperature high-pressure mixer 10 is avoided, and the safety of equipment is prevented from being influenced. And the range can avoid slurry returning blockage caused by filling the high-temperature high-pressure mixer with the coal-based solid waste slurry, stirring difficulty caused by uneven CO 2 distribution and premature coagulation of the coal-based solid waste slurry.|[0032] In another preferred embodiment, when the coal-based solid waste slurry is prepared, stirring is carried out at a speed of less than 60r/min for 6-10min, and stirring at a speed of less than 60r/min in the time range can avoid air mixing, so that the subsequent full permeation reaction with supercritical CO 2 is facilitated.|[0033] In another preferred embodiment, the supercritical CO 2 and coal-based solid waste slurry mixture is mixed and stirred at a speed of 300-400r/min for a period of 8-10min.|[0034] When the foam paste filling body master batch is depressurized after Wen Baoya, the pressure relief speed is controlled to be 2.5MPa/s, and the pressure in the high-temperature high-pressure mixer is gradually reduced to 0-7.4MPa.|[0035] The embodiment also provides the coal-based solid waste CO 2 foaming paste filling body prepared by the method for preparing the paste filling body with the carbon fixation and energy absorption functions based on SC-CO 2 foaming.|[0036] The preparation process described above is described in further detail below by way of specific examples.|[0037] When the preparation method of the embodiment is implemented, corresponding preparation equipment needs to be built, the preparation equipment can be equipment meeting the use condition in the prior art or equipment built according to the embodiment, as shown in fig. 2, the preparation equipment built according to the embodiment comprises a CO 2 air supply device 1, a high-temperature high-pressure reactor 4, a high-temperature high-pressure mixer 10, a curing oxidation chamber 12 and a constant-temperature box 13 which are sequentially connected through pipelines, wherein the tops of the CO 2 air supply device 1 and the high-temperature high-pressure reactor 4 are provided with a pressure gauge 2, the pipelines between the CO 2 air supply device 1 and the high-temperature high-pressure reactor 4 and the pipelines between the high-temperature high-pressure reactor 4 and the high-temperature high-pressure mixer 10 are respectively provided with a conveying valve 3, the high-temperature high-pressure mixer 10 is provided with a pressure sensor 6 and a temperature sensor 7 for detecting the internal pressure and the temperature of the high-temperature high-pressure mixer 10, the high-temperature high-pressure mixer 10 is further provided with a slurry feed port 9 and a pressure release valve 8, and the high-temperature high-pressure mixer 10 is internally provided with a stirring device 11 along the vertical direction.|[0038] As shown in FIG. 3, the high-temperature high-pressure reactor 4, the high-pressure pump 5, the pressure sensor 6, the temperature sensor 7, the pressure release valve 8, the slurry feed port 9, the high-temperature high-pressure mixer 10, the stirring device 11 and the curing maintenance chamber 12 are all arranged in the constant temperature box 13, so that all equipment in the experiment can be ensured to operate within a set temperature range, the interference of external temperature fluctuation on the experimental result can be avoided, and meanwhile, the sensor is matched for monitoring the temperature and the pressure change in the experiment in real time, so that a stable working environment is provided for the high-temperature high-pressure mixer 10 and the stirring device 11, the slurry is ensured to be fully mixed at an ideal temperature, and experimental errors caused by uneven temperature can be avoided. After the preparation equipment is built, crushing coal-based solid waste raw materials such as coal gangue and fly ash, grinding the crushed coal-based solid waste raw materials into powder with particle diameter of less than 20 mu m and particle ratio of more than 15%, stirring and mixing the powder with mixing water at a low speed of 60r/min for 6-10min, and obtaining coal-based solid waste slurry after stirring by adopting the low-speed stirring mode, wherein the prepared coal-based solid waste slurry waits to be injected into a high-temperature and high-pressure mixer;|[0039] The high temperature and high pressure mixer 10 is preheated to reduce the waiting time of the coal-based solid waste slurry injected later in the high temperature and high pressure mixer. |[0040] The high-temperature high-pressure reactor 4 is preheated to prevent pressure shock caused by temperature shock, the pressure and the temperature in the high-temperature high-pressure reactor 4 are regulated to ensure that the high temperature and the high pressure in the high-temperature high-pressure reactor 4 are kept in a high-temperature 31 ℃ range and the high pressure is kept in a 7.3MPa range, so that the pressure and the temperature in the process of converting gaseous CO 2 into supercritical CO 2 in the high-temperature high-pressure reactor 4 are cooperatively regulated;|[0041] the delivery valve between the CO 2 gas supply device 1 and the high-temperature high-pressure reactor 4 is opened, CO 2 is continuously injected into the high-temperature high-pressure reactor 4 through the pressure difference between the CO 2 gas supply device 1 and the high-temperature high-pressure reactor 4, the high-temperature high-pressure reactor 4 is in a vacuum state at this time, about-0.02 MPa, and the delivery valve is closed until the pressure in the high-temperature high-pressure reactor 4 is approximately the same as the pressure in the CO 2 gas supply device 1. |[0042] And (3) carrying out heat preservation and pressure maintaining on the gaseous CO 2 injected into the high-temperature high-pressure reactor 4 in the pressure temperature range (the high temperature is 31 ℃ and the high pressure is kept in the range of 7.3 MPa) until the gaseous CO 2 in the high-temperature high-pressure reactor 4 reaches the state of phase change and is converted into supercritical carbon dioxide, namely SC-CO 2.|[0043] Injecting the prepared coal-based solid waste slurry into a container through a slurry feed inlet above the high-temperature high-pressure mixer 10, completing injection when the injection volume is 1/3 of the volume of the high-temperature high-pressure mixer 10, and closing the coal-based solid waste slurry feed inlet to inject the coal-based solid waste slurry, wherein the inside of the high-temperature high-pressure mixer 10 is in a vacuum state of about-0.02 MPa;|[0044] In this embodiment, a stirring device 11 is vertically arranged inside the high-temperature and high-pressure mixer 10, the stirring device 11 in this embodiment is preferably a turbine type stirrer, and after the injection of the coal-based solid waste slurry is completed and the feeding port of the coal-based solid waste slurry is closed, a spiral stirring rod in the high-temperature and high-pressure mixer 10 is started to stir the injected coal-based solid waste slurry; |[0045] In the stirring process of the coal-based solid waste slurry, a conveying valve 3 between a high-temperature high-pressure reactor 4 and a high-temperature high-pressure mixer 10 is opened, a high-pressure pump is started, supercritical carbon dioxide, namely SC-CO 2, is continuously pumped into the high-temperature high-pressure mixer 10 at constant temperature and constant pressure in the stirring process, supercritical CO 2 is pumped into the mixer while stirring, and the conveying valve 3 is closed after the pressure of a CO 2 air supply device 1 is the same as that of the high-temperature high-pressure mixer 10. In the embodiment, CO 2 is continuously injected into the coal-based solid waste slurry in the stirring process, so that the compressive strength of the solidified filler can be improved; |[0046] Further, by adjusting and observing the pressure sensor 6 and the temperature sensor 7 above the high-temperature high-pressure mixer 10, the high-temperature high-pressure mixer 10 is kept in a heat preservation and pressure maintaining state, namely in a temperature 31 ℃ range, and supercritical CO 2 is fully permeated into the coal-based solid waste slurry within a pressure 7.3MPa range, so that a mixture of the supercritical CO 2 and the coal-based solid waste slurry is formed; |[0047] Then under the conditions of high pressure and high temperature, continuously stirring and mixing the mixture in the high temperature and high pressure mixer 10 by a spiral stirring rod, wherein the stirring speed is 300-400r/min, the stirring time is 8-10min, and the foam paste filling master batch is formed; |[0048] The heat preservation and pressure maintaining time of the foam paste filling body master batch formed after stirring is controlled to be 10min in the high-temperature high-pressure mixer 10, the pre-solidification of the coal-based solid waste slurry is avoided by controlling the pressure maintaining time, the sufficient fluidity of the coal-based solid waste slurry is ensured, a pressure relief valve 8 above the high-temperature high-pressure mixer 10 is opened, the pressure relief speed is controlled to be 2.5MPa/s, the pressure relief speed is not too fast, otherwise, the CO 2 in the high-temperature high-pressure mixer 10 generates dry ice to influence the foaming effect, the pressure in the high-temperature high-pressure mixer 10 is gradually reduced to 0MPa, at the moment, the SC-CO 2 in the high-temperature high-pressure mixer 10 is in a reduced pressure state condition, the CO 2 with larger density is desolventized, the CO 2 is converted into a gaseous state by supercritical, the CO 2 in the solution is released, the gas volume is rapidly expanded, a large amount of bubbles are formed, and the foaming of the paste filling body master batch is realized, and a large amount of the coal-based solid waste foaming filling body slurry taking supercritical CO 2 as a foam nucleus is formed. |[0049] The mineral substances in the slurry of the coal-based solid waste foaming paste filler are carbonated and hardened due to the dissolution of CO 2 and the reaction with water, so that the filler has better strength and durability, the number of pores with the diameter of more than 1000 nanometers is reduced due to the dissolution and chemical reaction effects of CO 2 bubbles, the compressive strength of the slurry of the coal-based solid waste foaming paste filler is enhanced, and the negative influence of the increase of the porosity on the slurry of the coal-based solid waste CO 2 foaming paste filler is reduced to the greatest extent;|[0050] And (3) injecting the slurry of the coal-based solid waste filling body in the high-temperature and high-pressure mixer into a curing chamber 12, and curing for a time to form the cured coal-based solid waste CO 2 foaming paste filling body. The original loose paste filling body is changed into a honeycomb-shaped (CO 2 cell structure) filling body with high strength, high elasticity and energy absorption property through the foaming process. |[0051] The development of supercritical CO 2 foam-filler porosity is affected by the diffusion-dissolution-reaction behavior of CO 2 in supercritical CO 2 -filler systems.|[0052] In the embodiment, density and porosity effect tests are carried out on the cured paste filling body with the carbon fixation and energy absorption functions, the cell morphology of the paste filling body with the carbon fixation and energy absorption functions is observed by a 3D microscope, and the test is carried out by a BSD-TD-K full-automatic true density and porosity analyzer, so that the density of the paste filling body with the carbon fixation and energy absorption functions is 35% -50% lower than that of the traditional cement-based filling material, and the porosity is 45% -80%, and the paste filling body with the carbon fixation and energy absorption functions is obviously superior to that of the traditional cementing filling body.|[0053] The energy absorption performance test verification is carried out on the cured CO 2 foaming coal-based solid waste filling body in the embodiment, the mine environment is simulated, the energy absorption characteristic of the CO 2 foaming coal-based solid waste filling body is tested by adopting a pressure sensor, and the result shows that the paste filling body with the carbon fixation and energy absorption functions prepared in the embodiment can absorb 50% -70% of energy of shock waves, and compared with the traditional filling body (such as cement and gypsum-based filling materials), the energy absorption effect is improved by 30% -50%.|[0054] In the embodiment, the carbon fixing function effect test verification is carried out on the cured paste filling body with the carbon fixing and energy absorbing functions, the X-ray diffraction (XRD) technology is adopted to test the paste filling body with the carbon fixing and energy absorbing functions, the mineralization reaction of CO and minerals in coal-based solid waste slurry is verified, the carbon fixing rate of the prepared CO 2 foaming coal-based solid waste filling body in the foaming process is 6-11%, and the carbon storage amount of cells is 1-2kg.|[0055] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. Family Number|(114513321)|114513321|Abstract|(CN119951390B B)|The invention discloses a method for preparing a paste filling body with carbon sequestration and energy absorption functions based on SC - CO2 foaming , and belongs to the technical field of coal mining . The preparation method comprises the following steps : crushing and grinding a coal - based solid waste raw material , and stirring and mixing the crushed and ground coal - based solid waste raw material with mixing water at a speed of less than 60 r / min to prepare coal - based solid waste slurry ; cO2 in a supercritical state is continuously injected during stirring until the pressure is the same as the set pressure , the supercritical CO2 permeates into the coal - based solid waste material slurry to form a mixture of the supercritical CO2 and the coal - based solid waste material slurry , the mixture of the supercritical CO2 and the coal - based solid waste material slurry is stirred and mixed in a turbo mode to form foam paste filling body master batch , and the foam paste filling body master batch is formed . The heat preservation and the pressure maintaining of the foam paste filling body master batch are controlled in a high - temperature and high - pressure mixer for 10-30 minutes , and then the pressure is quickly relieved , so that a large number of coal - based solid waste foam paste filling bodies taking supercritical CO2 as foam nucleuses are formed , the foaming of the paste filling body master batch is realized , and the filling body has low density , good heat insulation performance and a controllable foam pore structure . |IPC codes|(CN119951390B B)|B01F - 033/83 |Title|(CN119951390 A)|Method for preparing paste filling body with carbon sequestration and energy absorption functions based on SC - CO2 foaming | Chemical engineering|Civil engineering|Materials, metallurgy A01F-029/10|B01D-046/00|B01D-051/02|B02C-023/30|B28C-005/38/5|B28C-005/38/6|B28C-005/38/8|B64D-001/08|B67D-001/07|C02F-011/12/7|C04B-007/02|C04B-014/06|C04B-018/08|C04B-018/12|C04B-018/14/2|C04B-022/00/2|C04B-022/06/2|C04B-022/06/4|C04B-022/14/3|C04B-024/14|C04B-024/16|C04B-024/24|C04B-024/38/3|C04B-028/00|C04B-028/04|C04B-028/14|C04B-028/14/3|C04B-038/00/67|C04B-038/02|C04B-038/10|C04B-038/10/6|C04B-040/00/32|C04B-2103/0068|C04B-2103/12|C04B-2103/302|C04B-2103/42|C04B-2103/48|C04B-2111/00146|C04B-2111/00724|C04B-2111/40|C04B-2201/20|C04B-2201/32|C04B-2201/50|C08J-003/28|C08K-005/103|C08L-055/02|E04G-021/14|E21F-015/00|E21F-015/00/5|Y02P-020/54|Y02W-030/622 A01F-029/10|B01D-046/00|B01D-051/02|B02C-023/30|B28C-005/38/5|B28C-005/38/6|B28C-005/38/8|B64D-001/08|B67D-001/07|C02F-011/12/7|C04B-007/02|C04B-014/06|C04B-018/08|C04B-018/12|C04B-018/14/2|C04B-022/00/2|C04B-022/06/2|C04B-022/06/4|C04B-022/14/3|C04B-024/14|C04B-024/16|C04B-024/24|C04B-024/38/3|C04B-028/00|C04B-028/04|C04B-028/14|C04B-028/14/3|C04B-038/00/67|C04B-038/02|C04B-038/10|C04B-038/10/6|C04B-040/00/32|C04B-2103/0068|C04B-2103/12|C04B-2103/302|C04B-2103/42|C04B-2103/48|C04B-2111/00146|C04B-2111/00724|C04B-2111/40|C04B-2201/20|C04B-2201/32|C04B-2201/50|C08J-003/28|C08K-005/103|C08L-055/02|E04G-021/14|E21F-015/00|E21F-015/00/5|Y02P-020/54|Y02W-030/622 B01F-033/83|C04B-038/10|E21F-015/00 B01F-033/83|C04B-038/10|E21F-015/00 CN118405896|CN118005353|CN117658508|CN116575917|CN114426419|CN110218066|CN119321342 CN118405896 110841077 WHO=Examiner SELF=N CAT=A|CN118005353 109736767 WHO=Examiner SELF=N CAT=A|CN117658508 108801280 WHO=Examiner SELF=N CAT=A|CN116575917 106080354 WHO=Examiner SELF=N CAT=A|CN114426419 99868789 WHO=Examiner SELF=N CAT=A|CN110218066 85941814 WHO=Examiner SELF=N CAT=A|CN119321342 113081887 WHO=Examiner SELF=N CN116575917; CN117658508; CN118005353; CN118405896; CN110218066; CN114426419; CN119321342 GRANTED (CN119951390)|GRANTED ALIVE (CN119951390)|ALIVE (CN119951390)|LEGAL DETAILS FOR CN119951390|Actual or expected expiration date=2045-02-27|Legal state=ALIVE|Status=GRANTED|Event publication date=2025-02-27|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510226727|Application date=2025-02-27|Standardized application number=2025CN-0226727|Event publication date=2025-05-09|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119951390|Publication stage code=A|Publication date=2025-05-09|Standardized publication number=CN119951390|Event publication date=2025-05-09|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-05-27|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-11-18|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN119951390|Publication stage code=B|Publication date=2025-11-18|Standardized publication number=CN119951390B|Event publication date=2025-11-18|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN119951390)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoS/sFZvEddsOxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000079742183&ekey=2358&xpn=CN119951390B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=PpWciyKZ%252F0AQtvYjXtp5jLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN119951390)|CN|(CN119951390)|CN (CN119951390)|NAME=XI'AN UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN|(CN119951390)|NAME=XI'AN UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN119951390)|NAME=JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223|(CN119951390)|NAME=JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223 (CN119951390)|CN| (CN119951390)|NAME=YAN BAOXU, COUNTRY=CN |NAME=LIU PENGHAO|NAME=WANG ZEHANG|NAME=WANG BO|NAME=HE XIA|NAME=LIU YULIANG|NAME=JIA HANWEN|(CN119951390)|NAME=YAN BAOXU|NAME=LIU PENGHAO|NAME=WANG ZEHANG|NAME=WANG BO|NAME=HE XIA|NAME=LIU YULIANG|NAME=JIA HANWEN 0 1 Titre: (CN119951390)|SC-CO-based2Method for preparing paste filling body with carbon fixation and energy absorption functions through foaming Résumé: (CN119951390)|The invention discloses a method for preparing a paste filling body with carbon sequestration and energy absorption functions based on SC-CO2 foaming, and belongs to the technical field of coal mining. The preparation method comprises the following steps: crushing and grinding a coal-based solid waste raw material, and stirring and mixing the crushed and ground coal-based solid waste raw material with mixing water at a speed of less than 60r/min to prepare coal-based solid waste slurry; cO2 in a supercritical state is continuously injected during stirring until the pressure is the same as the set pressure, the supercritical CO2 permeates into the coal-based solid waste material slurry to form a mixture of the supercritical CO2 and the coal-based solid waste material slurry, the mixture of the supercritical CO2 and the coal-based solid waste material slurry is stirred and mixed in a turbo mode to form foam paste filling body master batch, and the foam paste filling body master batch is formed. The heat preservation and the pressure maintaining of the foam paste filling body master batch are controlled in a high-temperature and high-pressure mixer for 10-30 minutes, and then the pressure is quickly relieved, so that a large number of coal-based solid waste foam paste filling bodies taking supercritical CO2 as foam nucleuses are formed, the foaming of the paste filling body master batch is realized, and the filling body has low density, good heat insulation performance and a controllable foam pore structure. 44 Abstract gpt-4o-mini no The article focuses on a method for preparing a paste filling body using supercritical CO2 in coal mining, which does not involve the accelerated weathering of minerals or carbon sequestration through mineral carbonation.
45 CN202210008061 CN202210008061 CN114287302|CN114287302 99514297 CN114287302 B 2023-05-30 [CN114287302B]|CN114287302 A 2022-04-08 [CN114287302] 2022-01-06 2022-01-06 2023-05-30|2022-04-08 (CN114287302B)|2023-05-30 (CN114287302)|2042-01-06 (CN114287302)|Jidong coastal rice area machine-harvested rice carbon sequestration emission reduction, weight losing and synergy method (CN114287302)|The invention provides a method for carbon sequestration, emission reduction, weight loss and synergy of machine-harvested rice in a coastal rice area of East Hebei Province, which comprises the following steps: harvesting rice by using a harvester from the end of October to the first ten days of November, crushing straws, putting the crushed straws in situ, spreading a rice straw decomposing inoculant, and turning over; irrigating in a non-cultivation period until the soil saturation water content is reached; rotary tillage is conducted at the beginning of May in the second year, harrowing is conducted in the middle ten days of May, 450-600 kg/hm < 2 > of nitrogen-phosphorus-potassium slow-release fertilizer is applied to serve as base fertilizer, and sealing treatment is conducted 5-7 days before rice transplanting; transplanting is conducted in mid-to-late May, topdressing is conducted three times after transplanting, 97.5 kg/hm < 2 > of urea is topdressed for the first time, and 112.5 kg/hm < 2 > of urea is topdressed for the second time to the third time; and spraying pesticides for prevention and treatment before diseases and insect pests occur. According to the method, the resource utilization process of the rice straw is promoted, environmental pollution is reduced, the ecological environment is protected, good economic, ecological and social benefits are achieved, and green and sustainable development of agriculture is facilitated. BINHAI INSTITUTE OF AGRICULTURE HEBEI ACADEMY OF AGRICULTURE & FORESTRY SCIENCES (CN114287302)|BINHAI INSTITUTE OF AGRICULTURE HEBEI ACADEMY OF AGRICULTURE & FORESTRY SCIENCES ([CN])|(CN114287302)|BINHAI INSTITUTE OF AGRICULTURE HEBEI ACADEMY OF AGRICULTURE & FORESTRY SCIENCES ([CN]) LIU YAHUI|SUN JIANPING|ZHAO ZIJING|DAI XIANGLIN|DING FENGJIE|ZHANG WEI (CN114287302)|LIU YAHUI|SUN JIANPING|ZHAO ZIJING|DAI XIANGLIN|DING FENGJIE|ZHANG WEI|(CN114287302)|LIU YAHUI|SUN JIANPING|ZHAO ZIJING|DAI XIANGLIN|DING FENGJIE|ZHANG WEI (CN114287302)|ZHANG WEIHUA;XI'AN HUIEN INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 61244 (CN114287302)|Compared with the prior art, the invention has the following advantages:| (CN114287302)|1. A Jidong coastal rice harvesting carbon sequestration emission reduction, weight losing and synergy method is characterized by comprising the following steps:s1, crushing rice harvesting straws in autumn and returning the crushed straws to the field: harvesting rice in a harvester at the end of 10 months of the first year to the last ten days of 11 months, wherein the stubble height of the rice stubble is 10 cm-15 cm, crushing the straw into 5 cm-10 cm length, returning the whole amount of straw to the field to obtain returning straw, broadcasting a rice straw decomposing inoculant on the returning straw, and ploughing the rice straw decomposing inoculant, the returning straw and the rice stubble together; irrigation in the non-cultivation period to enable the soil to reach saturated water content;the rice straw decomposing inoculant is prepared from the following raw materials in parts by weight: 20 to 50 parts of termite fungus, 20 to 50 parts of trichoderma longibrachiatum, 20 to 50 parts of streptomyces fingii, 20 to 50 parts of staphylococcus, 10 to 30 parts of bacillus subtilis and 10 to 30 parts of bacillus mucilaginosus;the non-cultivation period in S1 refers to the period from when the rice straw decomposing inoculant, the returning straw and the rice stubble are ploughed together to when the rice straw is rotary tillage is performed;the returning amount of the returning straw in S1 is 18t/hm 2 ～25t/hm 2 The broadcast application amount of the rice straw decomposing inoculant is 30L/hm 2 ～45L/ hm 2 ;The ploughing depth in the step S1 is 10 cm-15 cm;s2, rotary tillage is carried out at the beginning of 5 months of the second year, raking is carried out in the middle of 5 months, and 450kg/hm of the rotary tillage is applied 2 ～600kg/hm 2 The slow-release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, and is subjected to sealing treatment before transplanting by using herbicide under the condition that the water layer is 5 cm-7 cm in 5-7 days before transplanting;s2, the mass fraction of N in the nitrogen-phosphorus-potassium slow release fertilizer is 25%, and P 2 O 5 Is 9% by mass, K 2 The mass fraction of O is 11%;s2, exposing 50-60% of soil blocks when raking;s3, selecting rice seedlings with the height of 10 cm-15 cm and the yellowish green leaves and white root systems for transplanting in the middle and late ten days of 5 months, wherein the transplanting density is 30cm multiplied by 16cm for each plant;s4, topdressing 3 times every 7 days after transplanting, 1 st timeTopdressing 97.5kg/hm 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a);s5, before the occurrence of rice diseases and insect pests, pesticide is sprayed for controlling.| (CN114287302)|Aiming at the defects of the prior art, the invention provides a carbon sequestration emission reduction, weight reduction and synergy method for harvesting rice in the Jidong coastal rice area, which is characterized in that the reasonable carbon sequestration emission reduction, weight reduction and synergy method for harvesting rice in the Jidong coastal rice area is constructed by carefully analyzing the precise fertilization of released nitrogen, phosphorus and potassium in the process of straw decomposition in the returning period, the non-cultivation period, the transplanting period and the straw decomposition period, thereby not only promoting the recycling process of rice straw, reducing environmental pollution and protecting ecological environment, but also having better economic, ecological and social benefits and being beneficial to the green and sustainable development of agriculture.|The invention provides a method for harvesting rice, fixing carbon, reducing emission, losing weight and enhancing efficiency in Jidonghai rice area, which comprises the following steps: harvesting rice in a harvester from the bottom of 10 months to the last ten days of 11 months, crushing the straw, then in situ, broadcasting a rice straw decomposing inoculant, and then turning over; irrigation in the non-cultivation period to reach the saturated water content of the soil; the first 5 months of the second year, raking the ground in the middle of 5 months and applying 450kg/hm 2 ~600kg/hm 2 The slow release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, and is sealed before transplanting for 5 to 7 days before transplanting; transplanting in middle and late 5 months, topdressing 3 times after transplanting, topdressing 97.5kg/hm 1 time 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a); before the occurrence of the plant diseases and insect pests, pesticide is sprayed for controlling.| (CN114287302)|EMISSION REDUCTION(100,16)|JIDONG COASTAL RICE AREA(100,11)|CARBON SEQUESTRATION(100,10)|SYNERGY(100,8)|CARBON SEQUESTRATION EMISSION REDUCTION(100,6)|JIDONG COASTAL RICE(100,3)|MACHINE HARVESTED RICE(100,1)|RICE AREA(100,1)|HARVESTING RICE(95,13)|JIDONG COASTAL RICE SYNERGY(84,1)|RICE STUBBLE(71,13)|RETURNING STRAW(69,19)|RICE STUBBLE HEIGHT(65,4)|BACILLUS MUCILAGINOSUS(63,16)|OXADIAZON MICROEMULSION(61,7)|RICE HARVEST SYNERGY(60,1)|ROTARY TILLAGE(57,11)|TERMITE FUNGUS(56,15)|RICE STRAW(52,42)|TRANSPLANT(52,21)|NONCULTIVATION PERIOD(48,18)|AGRICULTURE SUSTAINABLE DEVELOPMENT(48,3)|INOCULANT(47,25)|YELLOWISH GREEN LEAF(46,1)|LATE TEN DAY(43,1)|RELEASED NITROGEN PRECISE FERTILIZATION(43,1)|CRUSHED STRAW(40,4)|PYMETROZINE SUSPENDING AGENT(39,14)|ECOLOGICAL ENVIRONMENT(38,4)|JIDONGHAI RICE AREA(37,1)|STRAW DECOMPOSITION PERIOD(37,1)|TIMETOPDRESSING(37,1)|STRAW(36,34)|ENOXIME TEBUCONAZOLE(36,2)|RICE SEEDLING(35,6)|CRUSHING RICE(35,4)|TOP DRESSING(35,3)|ENESTROBURIN TEBUCONAZOLE SUSPENDING AGENT(35,2)|PYRACLOSTROBIN PENCONAZOLE SUSPENDING AGENT(35,2)|TRICHODERMA LONGIBRACHIATUM(34,16)|PLOWING(33,3)|PRECISE FERTILIZATION(33,2)|STRAW DECOMPOSITION(32,4)|CHLORANTRANILIPROLE SUSPENDING AGENT(30,6)|HARVESTER(30,5)|PHOSPHORUS(29,8)|BASE FERTILIZER(29,6)|TRANSPLANTING DENSITY(29,5)|PYRACLOSTROBIN SUSPENDING AGENT(29,4)|STUBBLE HEIGHT(29,4)|TRICYCLAZOLE SUSPENDING AGENT(28,8)|PESTICIDE(28,6)|UREA(27,11)|INSECT PEST(27,6)|IRRIGATION(26,9)|RECYCLING(26,3)|BACILLUS SUBTILIS(25,16)|PYRAZOSULFURON ETHYL WETTABLE POWDER(25,6)|TRICYCLAZOLE WETTABLE POWDER(24,4)|NITROGEN PHOSPHORUS POTASSIUM(24,3)|OXADIAZON PRETILACHLOR MICROEMULSION(24,3)|PESTICIDE SPRAYING(24,2)|SLOW RELEASE FERTILIZER(23,12)|BROADCAST(23,4)|ENVIRONMENTAL POLLUTION(23,3)|REDUCING ENVIRONMENTAL POLLUTION(23,1)|SUSTAINABLE DEVELOPMENT(21,3)|RELEASING NITROGEN(21,2)|TRANSPLANTING PERIOD(20,7)|FIXING CARBON(20,4)|SOCIAL BENEFIT(19,3)|ENESTROBURIN MASS FRACTION(19,2)|STRAW DECOMPOSITION(19,2)|UNMANNED AERIAL VEHICLE SPRAYING(19,2)|STAPHYLOCOCCUS(18,9)|STREPTOMYCES(18,7)|MASS FRACTION(17,24)|DOSAGE(17,10)|PRETILACHLOR MASS FRACTION(17,4)|PYRACLOSTROBIN MASS FRACTION(17,4)|JOINTING PERIOD(16,5)|RAKING(16,5)|OXADIAZON MASS FRACTION(16,4)|COASTAL AGRICULTURE COMPREHENSIVE(16,2)|PLANT DISEASE(16,2)|BOOTING(15,5)|PYRACLOSTROBIN TEBUCONAZOLE SUSPENSION(15,2)|LIQUID MEDICINE ATOMIZATION LEVEL(15,1)|SALINIZED COASTAL CLAY LOAM(15,1)|SOIL SATURATED WATER CONTENT(15,1)|AUTUMN(14,10)|RICE DISEASE(14,4)|GROUND(13,9)|HEADING MENSTRUATION(13,5)|FLYING SPEED(13,4)|HERBICIDE(13,4)|COASTAL MODERN AGRICULTURE COMPREHENSIVE(13,1)|SPRAY WIDTH(12,4)|WHITE ROOT(12,4)|FARMER HABIT FERTILIZATION(12,1)|ANNUAL PRECIPITATION(11,4)|PYMETROZINE SUSPENSION(11,4)|PYRACLOSTROBIN SUSPENSION(11,4)|DECOMPOSING INOCULANT(11,2)|DECREMENT FERTILIZATION(11,2)|DEOXIM TEBUCONAZOLE SUSPENDING AGENT(11,2)|STREPTOMYCES FINELEGAN(11,2)|COASTAL AGRICULTURAL COMPREHENSIVE(11,1)|STRICTLY PROHIBITED STRAW BURNING(11,1)|SLOW DECOMPOSITION(10,8)|AGRICULTURAL FUKANG STRAW(10,1)|COASTAL AGRICULTURAL INSTITUTE(10,1)|VIGOROUSLY ADVOCATED STRAW(10,1)|RETURN(9,13)|TILLERING SPEED(9,7)|WEIGHT REDUCTION(9,5)|DINICONAZOLE SUSPENDING AGENT(9,4)|CHLORANTRANILIPROLE SUSPENSION(9,2)|SOIL BLOCK(9,2)|WARM ZONE SEMIHUMID SEASON(9,1)|WATER LAYER(8,7)|FLYING HEIGHT(8,4)|LOSING WEIGHT(8,4)|TEST STATION ALTITUDE(8,3)|ANNUAL RICE STRAW YIELD(8,2)|NONCULTIVATION PERIOD MOISTURE MANAGEMENT(8,2)|SPRAYING PESTICIDE(8,2)|TRICYCLAZOLE SUSPENSION(8,2)|IMPACT ART DEFECT(8,1)|PRECISE FERTILIZATION METICULOUS ANALYSIS(8,1)|RETURNING STRAW DECOMPOSITION(8,1)|STRAW COMPREHENSIVE UTILIZATION(8,1)|STRAW DECOMPOSITION LAW(8,1)|UNREASONABLE FERTILIZER PROPORTION(8,1)|SATURATED WATER CONTENT(7,5)|REDUCING FERTILIZER(7,4)|IMPACT ART(7,2)|PLOWING DEPTH(7,2)|OFFSHORE CONTINENTAL CLIMATE(7,1)|SHI NONG FUKANG STRAW(7,1)|SYNCHRONOUS RAINY DAY(7,1)|TILLER FERTILIZER(7,1)|TRANSPLANTING SEEDLING(7,1)|EASTERN MONSOON AREA(6,3)|POTTING(6,3)|AGRICULTURAL STRAW(6,1)|FERTILIZATION MEASURE INFLUENCE(6,1)|FERTILIZER DECREMENT(6,1)|HARVESTING SEASON(6,1)|HEBEI PROVINCE(6,1)|MICROBIAL INOCULUM ACTION(6,1)|NONDISEASED RICE STRAW(6,1)|NONGFUKANG BIOTECHNOLOGY CO(6,1)|NONGFUKANG STRAW ACTION(6,1)|NYLON MESH BAG LANDFILL(6,1)|SOIL ECOSYSTEM(6,1)|SPIKE FERTILIZER(6,1)|STRAW DECOMPOSITION SAMPLE(6,1)|TIAN PEISHUI RICE STRAW(6,1)|SPIKE NUMBER(5,9)|TILLERING NUMBER(5,7)|FORESTRY(5,4)|NATIONAL ACADEMY(5,4)|ANNUAL AVERAGE TEMPERATURE(5,3)|MICROORGANISM(5,3)|SEALING TREATMENT(5,3)|YELLOW GREEN LEAVE(5,3)|DEWEIGHTING(5,2)|ATMOSPHERE ECOLOGICAL ENVIRONMENT(5,1)|DECOMPOSITION ACCELERATOR(5,1)|EXTENSIVE UTILIZATION(5,1)|FERTILIZATION TREATMENT INFLUENCE(5,1)|FUKAN STRAW(5,1)|GROUND THAWING(5,1)|IRRIGATION INFLUENCE(5,1)|IRRIGATION TREATMENT B2(5,1)|ISTHE STRAW(5,1)|LATE PLANTING(5,1)|LIQUID MEDICINE ATOMIZATION GRADE(5,1)|PADDY SOIL(5,1)|PADDY YUAN KG(5,1)|RICE TILLERING PERIOD(5,1)|RICE TRANSPLANTING(5,1)|SOIL VENTILATION(5,1)|STRAW QUICK DECOMPOSITION PERIOD(5,1)|URGENT TASK(5,1)|EAR FORMATION(4,2)|LAYER DRY LAND(4,2)|QUICK ACTING NITROGEN(4,2)|QUICK ACTING POTASSIUM(4,2)|RAPID DECOMPOSITION PERIOD(4,2)|REDUCING NITROGEN FERTILIZER(4,2)|ACCURATE FERTILIZATION(4,1)|CHEMICAL FERTILIZER HYPOAPPLICATION(4,1)|CONCENTRATED PRECIPITATION(4,1)|EARLY PLANTING(4,1)|LIQUID ATOMIZATION(4,1)|NONIRRIGATION TREATMENT(4,1)|QUALITY CULTIVATION(4,1)|RETURNING STRAW CONDITION(4,1)|SOIL DEEP PLOWING(4,1)|STRAW NATURAL DECOMPOSITION PERIOD(4,1)|TRANSPLANTING PERIOD INFLUENCE(4,1)|TREATMENT GROUP(3,16)|LACTATION PERIOD(3,4)|MASS RESIDUAL RATE(3,4)|AGRICULTURAL BIOTECHNOLOGY CO(3,1)|APPLYING NFK(3,1)|AVERAGE EVAPORATION CAPACITY(3,1)|BASIC SEEDLING(3,1)|CAO FEIDIAN REGION(3,1)|CONNECTEDPOLLUTION(3,1)|CONSTITUTION FACTOR(3,1)|DECOMPOSITIONTHE SLOW SPEED(3,1)|FAST DECOMPOSITION PERIOD(3,1)|LOWERCASE LETTER(3,1)|MATURING PERIOD(3,1)|MIDDLE TEN DAY(3,1)|NEXT YEAR MONTH(3,1)|NOXIOUS GAS(3,1)|NUTRIENT RESIDUAL RATE(3,1)|PROMOTION(3,1)|REST CULTIVATION PERIOD(3,1)|RICE FINAL YIELD(3,1)||(CN114287302)|EMISSION REDUCTION(100,17)|WEIGHT REDUCTION(100,15)|MACHINE HARVESTED RICE(100,14)|CARBON FIXATION(100,13)|JIDONG COASTAL RICE AREA(100,9)|OXACAO PRETILACHLOR MICROEMULSION(100,9)|MACHINE HARVESTING RICE(100,1)|DECOMPOSITION MICROBIAL INOCULUM(83,8)|PYRACLOSTROBIN VALERYL ISOVALERYL TEBUCONAZOLE(63,4)|RICE STUBBLE(62,13)|YIDONG COASTAL RICE AREA(61,2)|STREPTOMYCES FENLEEENSIS(58,2)|TRANSPLANT(52,18)|ROTARY TILLAGE(51,10)|RESOURCE UTILIZATION(46,3)|ALKENE OXIME TEBUCONAZOLE(45,8)|RICE STRAW(44,40)|NONCULTIVATION PERIOD(44,18)|BACILLUS MUCILAGINOSUS(44,8)|RICE TRANSPLANTING(43,4)|TIME2THE UREA(42,4)|TERMITE BACTERIUM(40,8)|HARVESTED RICE STRAW(40,4)|PYMETROZINE SUSPENDING AGENT(39,16)|MICROBIAL INOCULUM(39,8)|METICULOUS ANALYSIS(38,1)|HARVESTING RICE(37,4)|PESTICIDE SPRAYING(37,4)|RICE SEEDLING(36,6)|NITROGEN PHOSPHORUS POTASSIUM(35,9)|INSECT PEST(35,7)|LATE TEN DAY(34,2)|MECHANIZED RICE(33,1)|ACCURATE FERTILIZATION(32,2)|ECOLOGYTHE ENVIRONMENT(32,1)|JIDONG RICE(32,1)|SPRAYING PESTICIDE(32,1)|TRANSPLANTING DENSITY(30,4)|STRAW(29,33)|TOP DRESSING(29,10)|RETURNED STRAW(29,9)|CHLORANTRANILIPROLE SUSPENDING AGENT(29,8)|BASE FERTILIZER(29,6)|HARVESTER(29,6)|STUBBLE HEIGHT(29,4)|ECOLOGICAL ENVIRONMENT(29,2)|RELEASING NITROGEN(29,1)|PYRACLOSTROBIN SUSPENDING AGENT(28,8)|TRICYCLAZOLE SUSPENDING AGENT(28,8)|WHITE HAIR ROOT(28,2)|PLOWING(26,5)|INOCULANT(25,14)|PYRAZOSULFURON ETHYL WETTABLE POWDER(25,6)|NONCULTIVATION WATER MANAGEMENT(25,1)|TRICHODERMA LONGIBRACHIATUM(24,9)|TRICYCLAZOLE WETTABLE POWDER(24,4)|UPTURNED SOIL(24,4)|ENVIRONMENTAL POLLUTION(23,3)|REDUCING ENVIRONMENTAL POLLUTION(23,1)|HERBICIDE(22,8)|YELLOW GREEN LEAVE(22,3)|AGRICULTURE(21,7)|SUSTAINABLE DEVELOPMENT(21,3)|PLANT DISEASE(21,1)|RICE(20,25)|AUTUMN(20,8)|COASTAL AGRICULTURE COMPREHENSIVE(20,3)|DEFECT(20,1)|DOSAGE(19,16)|PESTICIDE(19,4)|SOCIAL BENEFIT(19,3)|CARBON FIXATION SOIL(19,1)|PREHARVEST(19,1)|STAPHYLOCOCCUS(18,9)|BACILLUS SUBTILIS(18,8)|AGRICULTURAL FUKANG STRAW(18,3)|STRAW DECOMPOSITION(18,2)|GROUND(17,17)|RICE DISEASE(16,4)|SHOREA RICE AREA(16,2)|SLOW RELEASE FERTILIZER(15,10)|BOOTING(15,5)|JOINT(15,4)|K2THE MASS FRACTION(15,4)|UREA(15,2)|SALINIZED COASTAL CLAY LOAM(15,1)|PHOSPHORUS(14,3)|SPRAY WIDTH(14,2)|FIELD RETURNING STRAW(13,11)|HEADING MENSTRUATION(13,5)|FENAMINSTROBIN(13,4)|FLYING SPEED(13,4)|MILK RIPENING PERIOD(13,4)|STREPTOMYCES ELEGAN(13,3)|LIQUID MEDICINE ATOMIZATION LEVEL(13,2)|ANNUAL PRECIPITATION(12,4)|OXADIAZON(12,4)|RIPARIAN RICE(12,3)|PRETILACHLOR MICROEMULSION(12,2)|CARBON SEQUESTRATION EMISSION REDUCTION(12,1)|COASTAL MODERN AGRICULTURAL COMPREHENSIVE(12,1)|PLANT AREA(11,4)|WATER LAYER(10,8)|TILLERING SPEED(9,8)|UNMANNED AERIAL VEHICLE(9,4)|TANGSHAN CITY(9,2)|REDUCED FERTILIZATION(8,9)|FLYING HEIGHT(8,4)|LIQUID MEDICINE ATOMIZATION GRADE(8,2)|COASTAL AGRICULTURE RESEARCH INSTITUTE(8,1)|SEEDLING TRANSPLANTING CULTIVATION MODE(8,1)|UNREASONABLE FERTILIZER PROPORTION(8,1)|SATURATED WATER CONTENT(7,5)|SPRAYING AMPLITUDE(7,2)|WARM TEMPERATE ZONE(7,2)|AGRICULTURAL FUKANG BIOLOGICAL SCIENCE(7,1)|CAOFEI COUNTY(7,1)|DECOMPOSING INOCULANT(7,1)|DECREMENT FERTILIZATION(7,1)|OFFSHORE CONTINENTAL CLIMATE(7,1)|OXAZACHLOR MICROEMULSION(7,1)|SEEDLING TRANSPLANTING DENSITY(7,1)|SOILTHE MICROAREA(7,1)|STAGE4AND N2O DISCHARGE(7,1)|STRAW NONRETURNING TREATMENT(7,1)|TILLER FERTILIZER(7,1)|HEADING RATE(6,5)|TEST STATION(6,5)|WATER MANAGEMENT(6,5)|CONSTITUENT FACTOR(6,3)|RICE YIELD(6,3)|BACILLUS PEPTOIDEUS(6,1)|DECOMPOSITION INOCULANT(6,1)|FORESTRY ACADEMY(6,1)|GRADUAL SLOW DECOMPOSITION(6,1)|IRRIGATION MOUNTING TILLERING(6,1)|LOSING WEIGHT(6,1)|NYLON MESH BAG LANDFILL(6,1)|PRECISE FERTILIZATION(6,1)|PROMOTED4THE EMISSION(6,1)|RICE CONSTITUTIVE FACTOR(6,1)|SOIL ECOSYSTEM(6,1)|SPIKE FERTILIZER(6,1)|STRAW DECOMPOSITION SAMPLE(6,1)|WATERTHE RICE STRAW(6,1)|EXPERIMENT(5,4)|ALTITUDE(5,3)|ANNUAL AVERAGE TEMPERATURE(5,3)|TRANSPLANTATION(5,3)|ANNUAL PRODUCTION(5,2)|CAO FEI DIAN REGION(5,2)|EAST QUARTER WIND REGION(5,2)|FERTILIZER REDUCTION(5,2)|K2O CONTENT(5,2)|STREPTOMYCES FINLAYI(5,2)|WARM ZONE(5,2)|ATMOSPHERIC ECOLOGICAL ENVIRONMENT(5,1)|EAST QUARTER WIND ZONE(5,1)|EXTENSIVE UTILIZATION(5,1)|FERTILIZATION MEASURE(5,1)|FERTILIZATION PRECISION(5,1)|INOCULANT RETURNING TREATMENT(5,1)|IRRIGATION TREATMENT B2(5,1)|POTTED PLANT TEST MICROAREA(5,1)|RESPLITTING ZONE(5,1)|RICE GREEN TURNING(5,1)|SEASON RICE STRAW(5,1)|SYNCHRONOUS RAIN(5,1)|URGENT TASK(5,1)|SPIKE NUMBER(4,6)|CLOSING TREATMENT(4,2)|HABIT(4,2)|MICROORGANISM(4,2)|PHYSICOCHEMICAL PROPERTY(4,2)|PLANT HEIGHT(4,2)|QUICK ACTING NITROGEN(4,2)|QUICK ACTING POTASSIUM(4,2)|RAPID DECOMPOSITION PERIOD(4,2)|TILLERING PERIOD(4,2)|WATER SOURCE(4,2)|CANADIAN ZONE(4,1)|CAREFUL ANALYSIS(4,1)|CONCENTRATED PRECIPITATION(4,1)|CUMULATIVE DISCHARGE(4,1)|DECOMPOSITION LAW(4,1)|FARMLAND QUALITY(4,1)|MTTHE RESIDUAL(4,1)|NONIRRIGATION TREATMENT(4,1)|NORTH RIVER(4,1)|POSITIONAL CRACKING ZONE TEST(4,1)|RESOURCE WASTE(4,1)|RICE PRICE(4,1)|RICE SOIL(4,1)|SEEDLING GROWTH(4,1)|STRAW SAMPLE(4,1)|TESTED DECOMPOSING(4,1)|MASS RESIDUE RATE(3,4)|AVERAGE EVAPORATION CAPACITY(3,1)|BASIC SEEDLING(3,1)|CAOFEI DIAN REGION(3,1)|DECOMPOSITION SLOW PERIOD(3,1)|DISEASE DAMAGE(3,1)|FAST DECOMPOSITION PERIOD(3,1)|FORMULA M0THE INITIAL(3,1)|MIDDLE TEN DAY(3,1)|MOUNTING FARMLAND(3,1)|NUTRIENT RESIDUAL RATE(3,1)|PLASTIC BARREL(3,1)|POTTING(3,1)|REST CULTIVATION PERIOD(3,1)|STRAW RESIDUE RATIO(3,1)|TECHNICAL ESSENCE(3,1)| (CN114287302)|1. A Jidong coastal rice harvesting carbon sequestration emission reduction, weight losing and synergy method is characterized by comprising the following steps:|s1, crushing rice harvesting straws in autumn and returning the crushed straws to the field: harvesting rice in a harvester at the end of 10 months of the first year to the last ten days of 11 months, wherein the stubble height of the rice stubble is 10 cm-15 cm, crushing the straw into 5 cm-10 cm length, returning the whole amount of straw to the field to obtain returning straw, broadcasting a rice straw decomposing inoculant on the returning straw, and ploughing the rice straw decomposing inoculant, the returning straw and the rice stubble together; irrigation in the non-cultivation period to enable the soil to reach saturated water content;|the rice straw decomposing inoculant is prepared from the following raw materials in parts by weight: 20 to 50 parts of termite fungus, 20 to 50 parts of trichoderma longibrachiatum, 20 to 50 parts of streptomyces fingii, 20 to 50 parts of staphylococcus, 10 to 30 parts of bacillus subtilis and 10 to 30 parts of bacillus mucilaginosus;|the non-cultivation period in S1 refers to the period from when the rice straw decomposing inoculant, the returning straw and the rice stubble are ploughed together to when the rice straw is rotary tillage is performed;|the returning amount of the returning straw in S1 is 18t/hm 2 ～25t/hm 2 The broadcast application amount of the rice straw decomposing inoculant is 30L/hm 2 ～45L/ hm 2 ;|The ploughing depth in the step S1 is 10 cm-15 cm;|s2, rotary tillage is carried out at the beginning of 5 months of the second year, raking is carried out in the middle of 5 months, and 450kg/hm of the rotary tillage is applied 2 ～600kg/hm 2 The slow-release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, and is subjected to sealing treatment before transplanting by using herbicide under the condition that the water layer is 5 cm-7 cm in 5-7 days before transplanting;|s2, the mass fraction of N in the nitrogen-phosphorus-potassium slow release fertilizer is 25%, and P 2 O 5 Is 9% by mass, K 2 The mass fraction of O is 11%;|s2, exposing 50-60% of soil blocks when raking;|s3, selecting rice seedlings with the height of 10 cm-15 cm and the yellowish green leaves and white root systems for transplanting in the middle and late ten days of 5 months, wherein the transplanting density is 30cm multiplied by 16cm for each plant;|s4, topdressing 3 times every 7 days after transplanting, 1 st timeTopdressing 97.5kg/hm 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a);|s5, before the occurrence of rice diseases and insect pests, pesticide is sprayed for controlling.|2. The method for carbon sequestration, emission reduction, weight loss and synergy of Jidong coastal rice district machine harvesting rice according to claim 1, wherein the herbicide in S2 is a mixture of 40% oxadiazon microemulsion and 10% pyrazosulfuron-ethyl wettable powder; the mass fraction of pretilachlor in the 40% oxadiazon microemulsion is 30%, and the mass fraction of oxadiazon is 10%; the dosage of the 40% oxadiazon micro-emulsion is 90 ml/mu to 100 ml/mu; the dosage of the 10% pyrazosulfuron-ethyl wettable powder is 15 g/mu-20 g/mu.|3. The method for harvesting rice, carbon sequestration, emission reduction, weight reduction and synergy in Jidong coastal rice area machine according to claim 1, wherein the method for sealing before insertion in S2 adopts unmanned aerial vehicle spraying, the spraying width is 10m, the flying height is 2.5m, the flying speed is 8m/S, and the liquid medicine atomization level is 550 microns.|4. The method for carbon sequestration, emission reduction, weight loss and synergy of mechanical rice harvest in Jidong coastal rice area according to claim 1, wherein the pesticide spraying in S5 is as follows:|spraying 200 g/L chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent with the dosage of 5 mL/mu in the jointing period;|spraying 20 mL/mu of 25% pyraclostrobin suspending agent, 40 g/mu of 75% tricyclazole wettable powder, 7.5 mL/mu of 200 g/liter chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent in the booting stage;|spraying 20 mL/mu of 25% pyraclostrobin suspending agent, 60 g/mu of 30% tricyclazole suspending agent and 20 g/mu of 25% pymetrozine suspending agent in the heading period;|spraying 25 mL/mu of 20% of enoxime tebuconazole suspending agent, 60 mL/mu of 30% of tricyclazole suspending agent and 20 g/mu of 25% of pymetrozine suspending agent in the period of lactation;|the mass fractions of pyraclostrobin and tebuconazole in the 25% pyraclostrobin-penconazole suspending agent are 12.5%; the mass fractions of the enestroburin and the tebuconazole in the 20% enestroburin-tebuconazole suspending agent are 10%. (CN114287302)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of comprehensive utilization of straw, and particularly relates to a method for harvesting rice, carbon sequestration, emission reduction, weight reduction and synergy in Jidong coastal rice areas.|BACKGROUND ART|[0002] The Jidong coastal rice area is a main rice producing area in Hebei province, and the planting area is about 100 ten thousand mu. The annual rice straw yield is about 70-80 ten thousand tons, and most of the annual rice straw yield is burnt due to the lack of efficient utilization technology, so that not only is the resource wasted and the soil ecosystem destroyed, but also the atmospheric pollution is caused. In recent years, the government has strictly prohibited straw burning and has vigorously advocated straw returning. It is known that straw returning is an effective measure for improving the organic carbon content of soil, but if returning is not reasonable, CH is greatly promoted 4 The emissions, and hence the increased greenhouse effect, will be higher than its carbon fixation effect. In the area, the temperature is low in winter and spring, and the straws return to the field for decompositionThe slow speed, especially the overlapping of the natural decomposition period of the straw and the turning green and tillering period of the rice, seriously inhibits the growth of seedlings, and becomes a main factor influencing the large-area popularization of the straw returning technology. In addition, the problems of unreasonable fertilizer proportion, low fertilizer application accuracy and the like exist in the rice planting process under the condition of returning the straw to the field, so that the fertilizer utilization rate is low, the cultivated quality is reduced, the emission of greenhouse gases is increased, and adverse effects are generated on farmlands and the ecological environment of the atmosphere. Therefore, establishing a reasonable carbon sequestration emission reduction and weight loss synergy technology is one of the urgent tasks in the current area.|DISCLOSURE|Disclosure of Invention|[0003] Aiming at the defects of the prior art, the invention provides a carbon sequestration emission reduction, weight reduction and synergy method for harvesting rice in the Jidong coastal rice area, which is characterized in that the reasonable carbon sequestration emission reduction, weight reduction and synergy method for harvesting rice in the Jidong coastal rice area is constructed by carefully analyzing the precise fertilization of released nitrogen, phosphorus and potassium in the process of straw decomposition in the returning period, the non-cultivation period, the transplanting period and the straw decomposition period, thereby not only promoting the recycling process of rice straw, reducing environmental pollution and protecting ecological environment, but also having better economic, ecological and social benefits and being beneficial to the green and sustainable development of agriculture.|[0004] In order to solve the technical problems, the invention adopts the following technical scheme: a Jidong coastal rice harvesting carbon sequestration emission reduction, weight losing and synergy method is characterized by comprising the following steps:|[0005] s1, crushing rice harvesting straws in autumn and returning the crushed straws to the field: harvesting rice in a harvester at the end of 10 months of the first year to the last ten days of 11 months, wherein the stubble height of the rice stubble is 10 cm-15 cm, crushing the straw into 5 cm-10 cm length, returning the whole amount of straw to the field to obtain returning straw, broadcasting a rice straw decomposing inoculant on the returning straw, and ploughing the rice straw decomposing inoculant, the returning straw and the rice stubble together; irrigation in the non-cultivation period to enable the soil to reach saturated water content;|[0006] the rice straw decomposing inoculant is prepared from the following raw materials in parts by weight: 20 to 50 parts of termite fungus (isoptercola sp.), 20 to 50 parts of trichoderma longibrachiatum (Trichoderma longibrachiatum), 20 to 50 parts of streptomyces fingii (Streptomyces finlayi), 20 to 50 parts of Staphylococcus (Staphylococcus sp.), 10 to 30 parts of bacillus subtilis (Bacillus subtilis) and 10 to 30 parts of bacillus mucilaginosus (Bacillus mucilaginosus);|[0007] s2, rotary tillage is carried out at the beginning of 5 months of the second year, raking is carried out in the middle of 5 months, and 450kg/hm of the rotary tillage is applied 2 ～600kg/hm 2 The slow-release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, and is subjected to sealing treatment before transplanting by using herbicide under the condition that the water layer is 5 cm-7 cm in 5-7 days before transplanting;|[0008] s3, selecting rice seedlings with the height of 10 cm-15 cm, yellow-green leaves and white roots for transplanting in the middle and late 5 months, wherein the transplanting density is 30cm multiplied by 16cm for each plant;|[0009] s4, dressing 3 times every 7 days after transplanting, wherein 97.5kg/hm is dressed 1 st time 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a);|[0010] s5, before the occurrence of rice diseases and insect pests, pesticide is sprayed for controlling.|[0011] Preferably, the non-cultivation period in S1 refers to a period from when the rice straw decomposing inoculant, the returning straw and the rice stubble are ploughed together to when the rice straw is rotary tillage.|[0012] Preferably, the returning amount of the returning straw in S1 is 18t/hm 2 ～25t/hm 2 The broadcast application amount of the rice straw decomposing inoculant is 30L/hm 2 ～45L/ hm 2 。|[0013] Preferably, the ploughing depth in the step S1 is 10 cm-15 cm.|[0014] Preferably, the mass fraction of N in the slow release fertilizer of nitrogen, phosphorus and potassium in S2 is 25%, P 2 O 5 Is 9% by mass, K 2 The mass fraction of O is 11%.|[0015] Preferably, the water layer is exposed from 50 to 60 percent of soil blocks during S2 raking.|[0016] Preferably, the herbicide in S2 is a mixture of 40% oxadiazon-pretilachlor microemulsion and 10% pyrazosulfuron-ethyl wettable powder; the mass fraction of pretilachlor in the 40% oxadiazon microemulsion is 30%, and the mass fraction of oxadiazon is 10%; the dosage of the 40% oxadiazon micro-emulsion is 90 ml/mu to 100 ml/mu; the dosage of the 10% pyrazosulfuron-ethyl wettable powder is 15 g/mu-20 g/mu.|[0017] Preferably, the method of sealing treatment before insertion in S2 adopts unmanned aerial vehicle spraying, the spraying width is 10m, the flying height is 2.5m, the flying speed is 8m/S, and the liquid medicine atomization grade is 550 microns.|[0018] Preferably, the spraying of the pesticide in S5 is:|[0019] spraying 200 g/L chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent with the dosage of 5 mL/mu in the jointing period;|[0020] spraying 20 mL/mu of 25% pyraclostrobin suspending agent, 40 g/mu of 75% tricyclazole wettable powder, 7.5 mL/mu of 200 g/liter chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent in the booting stage;|[0021] spraying 20 mL/mu of 25% pyraclostrobin suspending agent, 60 g/mu of 30% tricyclazole suspending agent and 20 g/mu of 25% pymetrozine suspending agent in the heading period;|[0022] spraying 25 mL/mu of 20% of enoxime tebuconazole suspending agent, 60 mL/mu of 30% of tricyclazole suspending agent and 20 g/mu of 25% of pymetrozine suspending agent in the period of lactation;|[0023] the mass fractions of pyraclostrobin and tebuconazole in the 25% pyraclostrobin-penconazole suspending agent are 12.5%; the mass fractions of the enestroburin and the tebuconazole in the 20% enestroburin-tebuconazole suspending agent are 10%.|[0024] Compared with the prior art, the invention has the following advantages:|[0025] the reasonable carbon fixation, emission reduction, weight reduction and synergy method for Jidong coastal rice areas is constructed through meticulous analysis of precise fertilization by releasing nitrogen, phosphorus and potassium in the returning period, the non-cultivation period moisture management, the transplanting period and the straw decomposition process, so that the recycling process of rice straw is promoted, the environmental pollution is reduced, the ecological environment is protected, better economic, ecological and social benefits are realized, and the green and sustainable development of agriculture is facilitated.|[0026] The invention is described in further detail below with reference to the drawings and examples.|DRAWINGS DESCRIPTION|[0027] Fig. 1 shows the residual straw ratios under different treatments according to example 3 of the present invention.|[0028] Fig. 2 shows temperature changes in the Cao Feidian region 2016-2020 of example 3 of the present invention.|INVENTION MODE|Detailed Description|Example 1|[0029] The test is carried out at a coastal agriculture comprehensive test station (39 DEG 17'40' 'N-118 DEG 27'22'' E) of the national academy of sciences of agriculture and forestry in Hebei province, the altitude of the test station is 2.5 meters, the test station belongs to the warm-warm zone semi-humid seasonal offshore continental climate in the eastern monsoon area, the annual average temperature is 11.4 ℃, the annual precipitation is 635.9mm, and the test station is concentrated in 7-8 months. The rice variety tested was Bindao 18.|[0030] The embodiment is a method for harvesting rice, fixing carbon, reducing emission, losing weight and enhancing efficiency in Jidong coastal rice areas, which comprises the following steps:|[0031] s1, crushing rice harvesting straws in autumn and returning the crushed straws to the field: harvesting rice by a harvester at the bottom of 10 months in the first year (10 months in 2020), wherein the stubble height of rice stubble is 10cm, crushing the straw into 5cm long, returning the whole straw to the field to obtain returning straw, spreading a rice straw rotting microbial inoculum on the returning straw, and ploughing the rice straw rotting microbial inoculum, the returning straw and the rice stubble together, wherein the ploughing depth is 10cm; irrigation in the non-cultivation period to enable the soil to reach saturated water content; the non-cultivation period refers to the period from when the rice straw decomposing inoculant, the returning straw and the rice stubble are ploughed together to when the rice straw is rotary tillage is performed; the returning amount of the returning straw is 25t/hm 2 The broadcast application amount of the rice straw returning decomposing inoculant is 45L/hm 2 ;|[0032] The rice straw returning decomposing inoculant is prepared from the following raw materials in parts by weight: 20 parts of termite fungus, 20 parts of trichoderma longibrachiatum, 20 parts of streptomyces fingii, 50 parts of staphylococcus, 30 parts of bacillus subtilis and 30 parts of bacillus mucilaginosus;|[0033] s2, rotary tillage is carried out at the beginning of 5 months (5 months and 5 days) of the second year, raking is carried out in the middle of 5 months (5 months and 12 days), and 600kg/hm of the fertilizer is applied 2 The slow-release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, a water layer is exposed at 50% soil when raking, the sealing treatment before transplanting is carried out by using herbicide under the condition that the water layer is 5cm 5 days before transplanting, unmanned aerial vehicle is adopted for spraying, the spraying width is 10m, the flying height is 2.5m, the flying speed is 8m/s, and the pesticide is preparedThe liquid atomization grade is 550 microns; the mass fraction of N in the nitrogen-phosphorus-potassium slow release fertilizer is 25%, and P is the same as that of the slow release fertilizer 2 O 5 Is 9% by mass, K 2 The mass fraction of O is 11%;|[0034] the herbicide is a mixture of 40% oxadiazon-pretilachlor microemulsion with the dosage of 90 ml/mu and 10% pyrazosulfuron-ethyl wettable powder with the dosage of 15 g/mu; the mass fraction of pretilachlor in the 40% oxadiazon microemulsion is 30%, and the mass fraction of oxadiazon is 10%;|[0035] s3, selecting rice seedlings with the height of 10 cm-15 cm and the yellow-green leaves and white roots for transplanting in the middle ten days of 5 months (19 days of 5 months), wherein the transplanting density is 30cm multiplied by 16cm for each plant area;|[0036] s4, dressing 3 times every 7 days after transplanting, wherein 97.5kg/hm is dressed 1 st time 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a);|[0037] s5, before the occurrence of rice diseases and insect pests, spraying pesticides for control, and spraying 200 g/L chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent at the jointing period;|[0038] spraying 20 mL/mu of 25% pyraclostrobin suspension, 40 g/mu of 75% tricyclazole wettable powder, 7.5 mL/mu of 200 g/liter chlorantraniliprole suspension and 20 g/mu of 25% pymetrozine suspension in the booting stage;|[0039] spraying 20 mL/mu of 25% pyraclostrobin suspension, 60 g/mu of 30% tricyclazole suspension and 20 g/mu of 25% pymetrozine suspension in the heading period;|[0040] spraying 20% of diniconazole suspending agent, 30% of tricyclazole suspending agent and 25% of pymetrozine suspending agent, wherein the concentration of diniconazole suspending agent is 25 mL/mu, the concentration of tricyclazole suspending agent is 60 mL/mu, and the concentration of pymetrozine suspending agent is 20 g/mu in the lactation period;|[0041] the mass fractions of pyraclostrobin and tebuconazole in the 25% pyraclostrobin-tebuconazole suspension are 12.5%; the mass fractions of the deoxim-methyl and the tebuconazole in the 20% deoxim-tebuconazole suspending agent are 10%.|[0042] The test adopts a single factor test and sets a comparison, CK is not returned to the field, the treatment is respectively set as T1-T3, T1 is returned to the field under the action of HT20 (the rice straw decomposing inoculant of the embodiment), and T2 isThe straw returning to the field under the action of the Nongfukang straw returning decomposition agent (commercially available from Nongfukang biotechnology Co., ltd.) and T3 is the returning to the field without the decomposition agent. Irrigation is carried out in a proper amount in a non-cultivation period, transplanting is carried out for 5 months and 21 days, and the fertilizer application scheme in the cultivation period is as follows: the CK straw is not returned to the field and is treated by conventional fertilization, T1-T3 adopts a fertilizer reducing scheme (table 1), the base fertilizer is applied once, the tiller fertilizer is applied in three times, and the first 97.5kg/hm 2 The latter two times are respectively 112.5kg/hm 2 The spike fertilizer is applied when the spike length reaches 0.3-0.5 cm. The pesticide and the water management measure are the same as the conventional method. The cell area is 744m 2 (18.6X10 m). CH was measured at 10-day intervals at tillering stage 4 And N 2 O emission, yield and soil organic matter content were measured during harvest.|[0043] TABLE 1 chemical fertilizer hypo-application scheme|[0044] |[0045] TABLE 2 yield and soil organic matter content|[0046] |[0047] Note that: the different lowercase letters in the tables indicate that the differences reach a significant level P <0.05, as in the following tables.|[0048] TABLE 3 tillering stage CH 4 And N 2 Accumulated O discharge|[0049] |[0050] After the method is applied, compared with the conventional fertilization without returning the straw to the field, not only the fertilizer application reduction is realized, but also the carbon fixation and emission reduction of the rice field, the rice yield and benefit increase (tables 2 and 3) are realized, the organic content of the soil is improved by 13.36-37.79%, and the CH at the tillering stage is improved 4 And N 2 The accumulated O discharge amount is respectively reduced by 61.86 percent and 56.67 percent; according to the price of 2.6 yuan/kg of paddy, the rice straw decomposing inoculant of the embodiment is applied to the field on the basis of 26.5% of fertilizer decrement, the yield of rice per mu is increased by 2.26%, and the cost per mu is saved by 131.12 yuan.|[0051] Example 2|[0052] The experiment was performed in 2020-2021 on four farms in Cao Feidian area of Tangshan, hebei province. Physical and chemical properties of 0-20cm plough layer soil in test field: the total salt content is 1.39 g/kg, the pH value is 7.51, the organic matter content is 18.56g/kg, and the quick-acting phosphorus content is 20.13g/kg. Quick-acting potassium 255.12 mg/kg and quick-acting nitrogen 78.81 mg/kg.|[0053] The embodiment is a method for harvesting rice, fixing carbon, reducing emission, losing weight and enhancing efficiency in Jidong coastal rice areas, which comprises the following steps:|[0054] s1, crushing rice harvesting straws in autumn and returning the crushed straws to the field: harvesting rice in the first 11 th (11 th of 2020), wherein the stubble height of the rice stubble is 15cm, crushing the straw into 8cm long, returning the whole amount of straw to the field to obtain returning straw, broadcasting a rice straw rotting microbial inoculum on the returning straw, and ploughing the rice straw rotting microbial inoculum, the returning straw and the rice stubble together, wherein the ploughing depth is 15cm; irrigation in the non-cultivation period to enable the soil to reach saturated water content; the non-cultivation period refers to the period from when the rice straw decomposing inoculant, the returning straw and the rice stubble are ploughed together to when the rice straw is rotary tillage is performed; the returning amount of the returning straw is 18t/hm 2 The broadcast application amount of the rice straw decomposing inoculant is 30L/hm 2 ;|[0055] The rice straw returning decomposing inoculant is prepared from the following raw materials in parts by weight: 50 parts of termite fungus, 50 parts of trichoderma longibrachiatum, 50 parts of streptomyces fingii, 20 parts of staphylococcus, 10 parts of bacillus subtilis and 10 parts of bacillus mucilaginosus;|[0056] s2, rotary tillage is carried out at the beginning of 5 months (5 months and 8 days) of the second year, raking is carried out in the middle of 5 months (5 months and 15 days), and 450kg/hm of the fertilizer is applied 2 The slow-release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, a water layer is exposed by 60% soil when raking, the sealing treatment before transplanting is carried out by using herbicide under the condition that the water layer is 7cm in 7 days before transplanting, the spraying width is 10m, the flying height is 2.5m, the flying speed is 8m/s, and the atomization level of the liquid medicine is 550 microns; the mass fraction of N in the nitrogen-phosphorus-potassium slow release fertilizer is 25%, and P is the same as that of the slow release fertilizer 2 O 5 Is 9% by mass, K 2 The mass fraction of O is 11%;|[0057] the herbicide is a mixture of 40% oxadiazon-pretilachlor microemulsion with the dosage of 100 ml/mu and 10% pyrazosulfuron-ethyl wettable powder with the dosage of 20 g/mu; the mass fraction of pretilachlor in the 40% oxadiazon microemulsion is 30%, and the mass fraction of oxadiazon is 10%;|[0058] s3, in the next ten days of 5 months (23 days of 5 months), selecting rice seedlings with the height of 10 cm-15 cm, yellow-green leaves and white roots for transplanting, wherein the transplanting density is 30cm multiplied by 16cm for each plant area;|[0059] s4, dressing 3 times every 7 days after transplanting, wherein 97.5kg/hm is dressed 1 st time 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a);|[0060] s5, before the occurrence of rice diseases and insect pests, spraying pesticides for control, and spraying 200 g/L chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent at the jointing period;|[0061] spraying 20 mL/mu of 25% pyraclostrobin suspension, 40 g/mu of 75% tricyclazole wettable powder, 7.5 mL/mu of 200 g/liter chlorantraniliprole suspension and 20 g/mu of 25% pymetrozine suspension in the booting stage;|[0062] spraying 20 mL/mu of 25% pyraclostrobin suspension, 60 g/mu of 30% tricyclazole suspension and 20 g/mu of 25% pymetrozine suspension in the heading period;|[0063] spraying 20% of diniconazole suspending agent, 30% of tricyclazole suspending agent and 25% of pymetrozine suspending agent, wherein the concentration of diniconazole suspending agent is 25 mL/mu, the concentration of tricyclazole suspending agent is 60 mL/mu, and the concentration of pymetrozine suspending agent is 20 g/mu in the lactation period;|[0064] the mass fractions of pyraclostrobin and tebuconazole in the 25% pyraclostrobin-tebuconazole suspension are 12.5%; the mass fractions of the deoxim-methyl and the tebuconazole in the 20% deoxim-tebuconazole suspending agent are 10%.|[0065] The average mu yield of the rice is 802 kg/mu, and the average organic matter content of the soil is 26.74g/kg.|[0066] Example 3|[0067] The embodiment is a test established for a method for harvesting rice, fixing carbon, reducing emission, losing weight and enhancing efficiency in Jidong coastal rice area:|[0068] the research area is located in an agricultural test field (N39 DEG 16 '31', E118 DEG 27 '5.14') of a coastal modern agriculture comprehensive test station in Tang Shanshi Cao Feidian area, belongs to an offshore continental climate in a warm and warm zone semi-humid season in an eastern quarter wind area, and has the climatic characteristics of sufficient illumination, concentrated precipitation, synchronous rainy and hot days, distinct dry and wet seasons and the like. The average annual temperature is 11.4 ℃, the average evaporation capacity is 1969mm, the annual precipitation is 635.9mm, and the method is mainly concentrated in 7-8 months. The soil type of the test land is paddy soil, and the physical and chemical properties of 0-20cm plough layer soil are as follows: the total salt content is 1.26 g/kg, the pH value is 7.65, the organic matter is 17.94g/kg, the total nitrogen is 1.13 g/kg, and the quick-acting phosphorus is 19.90 mg/kg. Quick-acting potassium 242.32 mg/kg and quick-acting nitrogen 73.11 mg/kg.|[0069] The area is planted with single-season rice, the test material is 18, the growth period is 170-175 days, the transplanting mode is adopted, and the transplanting density is 30 multiplied by 16cm. The 3 test decomposing agents were HT20 (rice straw decomposing inoculant in example 1: 20 parts of termite fungus, 20 parts of Trichoderma longibrachiatum, 20 parts of Streptomyces fingii, 50 parts of staphylococcus, 30 parts of bacillus subtilis and 30 parts of bacillus mucilaginosus), and the agricultural straw returning decomposing agent (commercially available, agricultural biotechnology Co., ltd., NFK for short).|[0070] Test one: non-cultivation period moisture management, returning period and transplanting period selection test|[0071] The test sets a return to field D1 after harvesting the rice and a return to field D2 after soil thawing in spring of the next year. The three-split zone test is adopted, the application conditions of returning to the field and the microbial inoculum are the main factors A, the three-split zone test comprises 4 levels, and A1 to A4 are respectively the control of returning to the field by applying HT20, returning to the field by applying NFK, returning to the field without applying the microbial inoculum and returning to the field by not applying the microbial inoculum. The water management in the non-cultivation period (the time from returning straw, microbial inoculum and rice stubble to tillage together to rotary tillage) is a side factor B, and comprises 2 levels, B1 is not irrigated, B2 is irrigated, so that the water content of soil is close to the saturation state, and the water is not irrigated in a flood mode. The transplanting period is a side factor C, and comprises 3 levels, C1 early planting (about 5 months and 15 days), C2 conventional (5 months and 22 days), C3 late planting (5 months and 29 days), and fertilizer, pesticide and water management measures in the rest cultivation period are the same as conventional measures. The main area is 166m 2 The area of the secondary region is 83m 2 The area of the re-cracking zone is 25m 2 Repeated 3 times. Plant height and basic seedling per hole are investigated on day 7 after transplanting, and hanging is carried out per cellThe method comprises the steps of 10 points are investigated, the plant height and the tillering number of each point are investigated every 7 days after the 10 points are investigated, until tillering is stopped, and the effective spike number of rice is recorded.|[0072] Results and analysis|[0073] 1. Influence of irrigation in different returning period and non-cultivation period on rice tillering and ear forming|[0074] Table 4 shows that the returning period has obvious influence on the highest tillering number, tillering speed, effective spike number and spike forming rate of rice, and the returning D1 in autumn is obviously higher than that in spring. The irrigation in the non-cultivation period has obvious influence on the highest tillering number, and the highest tillering number of the irrigation treatment B2 is higher than that of the non-irrigation treatment, but has no obvious influence on the effective spike number, the spike forming rate and the tillering speed. Therefore, in autumn, the optimal returning period is adopted, and the water can be properly irrigated in the non-cultivation period in the area with sufficient water source, so that the flood irrigation of large water is avoided.|[0075] TABLE 4 tillering and ear formation rates of Rice under different moisture management at different returning to field and non-cultivation periods|[0076] |[0077] 2. Influence of different transplanting periods on rice tillering and ear forming|[0078] The different transplanting periods have a large influence on the highest tillering number, tillering speed, effective spike number and spike forming rate (Table 5), wherein the highest tillering number is represented by C1 > C2 > C3, the tillering speed is represented by C3 > C1 > C2, the effective spike number is represented by C2 > C1 > C3, and the spike forming rate is represented by C3 > C2 > C1. Overall analysis, C2 is a more suitable transplanting period.|[0079] TABLE 5 tillering and ear formation rates of Rice at different transplanting periods|[0080] |[0081] Influence of returning to field of different microbial inoculum on rice tillering and ear forming rate|[0082] The application of different microbial inoculum to the field has great influence on the highest tillering speed, effective spike number and spike forming rate of rice (Table 6). The highest tillering speed, the effective spike number and the spike forming rate under the A1 treatment are obviously higher than those of the rest treatment, wherein the highest tillering speed is expressed as A1 & gtA 4 & gtA 2 & gtA 3, the effective spike number is expressed as A1 & gtA 2 & gtA 4 & gtA 3, and the spike forming rate is expressed as A1 & gtA 2 & gtA 4 & gtA 3. As can be seen, the effect of the microbial inoculum A1 is best.|[0083] Table 6 tillering and ear forming rates of returning rice under the action of different microbial inoculum|[0084] |[0085] In conclusion, when HT20 is applied to the field in autumn, water source sufficient areas can be supplied and irrigated appropriately after returning to the field and plowing, and then seedling transplanting is carried out in the middle and late 5 months of the next year, so that the highest tillering number, the effective spike number and the spike forming rate of the rice are improved greatly.|[0086] (II) test II: accurate fertilization scheme determination|[0087] The test is carried out at a coastal agriculture comprehensive test station (39 DEG 17'40' 'N-118 DEG 27'22'' E) of the national academy of sciences of agriculture and forestry in Hebei province, the altitude of the test station is 2.5 meters, the test station belongs to the warm and warm zone semi-humid seasonal offshore continental climate of the eastern monsoon area, the annual average temperature is 11.4 ℃, the annual precipitation is 635.9mm, and the test station is concentrated in 7-8 months.|[0088] The rice variety tested was Bindao 18. Urea (N content 46%), 45% methoprene (N content 25%, P) 2 O 5 Content 9%, K 2 O content 11%), potassium sulfate (K) 2 50% of O content), 50% of silicon grain slow release fertilizer (25% of N content, P) 2 O 5 10% of K 2 O content 15%).|[0089] Transplanting at 11 months 2020, 21 months 2021 and 10 months 2021. The previous crop is rice, and HT20 (20 parts of termite fungus, 20 parts of trichoderma longibrachiatum, 20 parts of streptomyces finelegans, 50 parts of staphylococcus, 30 parts of bacillus subtilis and 30 parts of bacillus mucilaginosus) is sprayed on the straw in the harvesting season, and then the cultivation returning treatment is carried out, wherein the cultivation returning depth is 10-15cm, and the water content of the soil is nearly saturated by irrigation.|[0090] The test sets 4 treatments of conventional fertilization and decrement fertilization (see table 7 for details), the conventional fertilization T1 mainly simulates the habit fertilization of farmers; reducing fertilizer T2, reducing fertilizer 17.42%, reducing nitrogen fertilizer 6.45%; reducing fertilizer T3, reducing fertilizer 26.51%, reducing nitrogen fertilizer 20.28%; the fertilizer is reduced by T4, 34.90 percent and 26.09 percent. Each treatment was repeated 3 times and randomly arranged. The field management is consistent with the conventional management.|[0091] Table 7 fertilization scheme|[0092] |[0093] Results and analysis|[0094] 1. Rice yield constitution factor|[0095] Under the condition of returning the straw to the field, the influence of different fertilization measures on the rice yield constituent factors is shown in table 8, and significant differences exist among the yield constituent factors of each treatment group. The effective spike number of the T3 treatment group is 16.11, which is higher than that of the other three treatment groups, and is respectively improved by 8.19 percent, 12.89 percent and 9.93 percent compared with the T1, the T2 and the T4, and is obviously higher than that of the T2 treatment group. The setting rate of the T3 treatment group is 94.72%, which is obviously higher than that of the conventional fertilization T1 treatment group, and is improved by 1.23% compared with T1, and the setting rates of T2 and T4 are respectively 94.14% and 94.52%, which are not obviously different from the other three groups. The spike grain number of the T2 treatment group is significantly higher than that of the other three treatment groups, namely 339.12, and is respectively 10.5%, 3.7% and 5.6% higher than that of the other three treatment groups. The T3 treatment group had higher effective spike number and higher seed setting than the other three treatment groups. The thousand grain weights of four different treated rice plants are not significantly different and all are about 32 g.|[0096] TABLE 8 influence of different fertilization treatments on Rice composition factors under straw returning|[0097] |[0098] 2. Influence on the yield of rice|[0099] Under the condition of returning straw to field, the rice yield of the conventional fertilization T1 treatment group is 9353 kg/hm 2 The final yield of the rice in the three treatment groups of decrement fertilization T2, T3 and T4 is higher than that of the rice in the conventional fertilization T1 treatment group, which are 9951 kg/hm respectively 2 、10953 kg/hm 2 、10110 kg/hm 2 The yield is increased by 6.39%, 17.11% and 8.09% respectively. The yield increasing effect of the deweighting T3 treatment group is most remarkable and is higher than that of the deweighting T2 and T4 treatment groups.|[0100] (III) test III: research on decomposition law of straw after returning to field|[0101] The potting test is carried out at a coastal agricultural comprehensive test station (39 DEG 17'40' N-118 DEG 27'22' E) of the national academy of sciences of agriculture and forestry in Hebei province, the altitude of the test station is 2.5 meters, the potting test belongs to the warm and warm zone semi-humid seasonal offshore continental climate of the eastern monsoon area, the annual average temperature is 11.4 ℃, the annual precipitation is 635.9mm, and the potting test is concentrated in 7-8 months. The soil type is salinized coastal clay loam, and rice is planted for many years.|[0102] The rice variety is 18, the growth period is 170 days, and the rice is bred by the coastal agricultural institute of the national academy of sciences of agriculture and forestry in Hebei province. The rice straw is a local non-diseased rice straw containing 0.68% of nitrogen (N) and 0.68% of phosphorus (P) 2 O 5 ) 0.13% and potassium (K) 2 O) 1.34%, C/N67, and crushing rice straw into about 5cm by a crusher. The decomposing inoculants were HT20 (rice straw returning decomposing inoculants in example 1: termite fungus 20 parts, trichoderma longibrachiatum 20 parts, streptomyces fenti 20 parts, staphylococcus 50 parts, bacillus subtilis 30 parts, and Bacillus mucilaginosus 30 parts) and Fukan straw returning decomposing inoculants (commercially available), respectively.|[0103] Adopting a random granule design, setting 3 treatment groups which are respectively:|[0104] (1) Returning the straw to the field directly-CK;|[0105] (2) Straw also Tian Peishui rice straw the rice straw returning to field decomposing inoculant (HT 20) -JH of example 1;|[0106] (3) The straw returning is matched with a Shi Nong Fukang straw returning decomposing agent-JF;|[0107] in order to simulate field production environment, potting test micro-areas are established, each micro-area has the specification of 600cm (length) x 200cm (width) x 60cm (depth), a plastic bucket (specification of 56 x 58 cm) is filled, holes are punched at the periphery and bottom of the bucket to ensure ventilation of soil and outflow of water, gaps between the buckets are filled with soil, and each treatment is arranged in one micro-area to prevent the micro-areas from being mutually connectedPollution, reduced test error, 3 micro-areas are 3 times repeated. The test used a nylon mesh bag landfill method, the nylon mesh bag specification was length x width=50 cm x 45cm, and the aperture was 0.178mm to isolate soil. 262g (10500 kg/hm of rice straw in each bag 2 And (5) returning the total amount of the straw to the field). Each treatment is applied to soil deep ploughing in the 11 th month and 25 th 2019, and rice seedlings are transplanted in the 5 th month and 28 th 2020, 5 holes are formed in each pot, and 5 plants are planted in each hole. Production management of weeding, irrigation, plant diseases and insect pests and the like is carried out according to local habits. The rice was harvested at 10 months and 10 days 2020.|[0108] Straw samples were collected 180, 210, 225, 240, 255, 265 and 295 days after returning to the field, respectively, 7 sampling times were positive to the rice transplanting period (28 days in 5 months in 2020), the tillering period (15 days in 6 months in 2020), the jointing period (28 days in 6 months in 2020), the booting period (25 days in 7 months in 2020), the heading period (5 days in 8 months in 2020), the milk ripening period (20 days in 8 months in 2020), and the maturing period (8 days in 10 months in 2020). And 5 pots are taken each time, the straw decomposition samples are dried to constant weight at 65 ℃, and the residual rate of the rice straw is calculated. The mass residual rate and the nutrient residual rate are calculated according to the following formulas:|[0109] mass residual rate (%) =m t /M 0 ,|[0110] M in the formula 0 The initial mass of the straw before decomposition;|[0111] M t is the residual mass of the decomposed straw at t.|[0112] Results and analysis|[0113] The quality residual rate of each treated straw is reduced along with the prolongation of the decomposition time, and the straw has the characteristics of quick decomposition in the early stage and gradual and slow decomposition in the later stage, and the difference exists between different treatments (figure 1). As can be seen, the treatment with HT20 (the rice straw returning to field decomposing inoculant comprises 20 parts of termite fungus, 20 parts of trichoderma longibrachiatum, 20 parts of streptomyces finyi, 50 parts of staphylococcus, 30 parts of bacillus subtilis and 30 parts of bacillus mucilaginosus) is within 0-180 days, the mass residual rate is rapidly reduced, the rapid decomposition period is 180-225 days, the slow decomposition period is 225-295 days, the mass residual rate is basically unchanged, and the decomposition stagnation period is reached. The control treatment belongs to the fast decomposition period within 0-240 days, the slow decomposition period is 240-255 days, and the slow decomposition period is 255-295 days. The treatment of the agricultural Fukang straw returning decomposing inoculant is carried out in a rapid decomposition period within 0-225 days, a slow decomposition period within 225-240 days and a slow decomposition period within 240-295 days. Therefore, the application of the rice straw returning and decomposing inoculant for returning the rice straw to the field can accelerate the decomposition of the returning straw, the quick decomposition period of the straw is finished before transplanting, the straw enters the slow decomposition period after transplanting, the harm of a large amount of harmful gases generated by the quick decomposition to rice seedlings is reduced, and compared with the control and other decomposing inoculants, the straw returning and decomposing inoculant for returning the rice straw to the field can enter the slow decomposition period 45-60 days in advance.|[0114] As can be seen from fig. 2, the temperature change in the area Cao Feidian in 2016-2020, combined with the residual rate of the straw in different treatments, can be known that HT20 returning treatment is performed in autumn, the average temperature during returning is 6.14 ℃ within 180 days after returning, that is, the period of time is 5 months after returning, and the rest of treatment is performed within 225-240 days after returning, that is, the period of time is 7-8 months, the average temperature is 12.65 ℃, so that HT20 can be started at a lower temperature (about 6 ℃) and straw decomposition is accelerated by microbial activity. The autumn returning is better than the spring returning, from the temperature of Cao Feidian in recent years, the average temperature of 11 months is below 5.5 ℃, the average temperature of 12-1 month is above zero, the average temperature of 2 months begins to rise to above zero, the average temperature of 3 months is 7 ℃, if the rice is harvested and the HT20 returning is carried out after about 11 months, the temperature is about 5 ℃, microorganisms can be started, a certain promotion effect on straw decomposition is achieved, then the microorganisms are frozen and thawed after three months, the temperature rises to 3 months, the microorganisms start to move again, and on the basis of decomposition before sealing, the straw starts to accelerate decomposition, and compared with the spring returning, the autumn returning is more beneficial to the spring returning.|[0115] The above description is only of the preferred embodiments of the present invention, and is not intended to limit the present invention. Any simple modification, variation and equivalent variation of the above embodiments according to the technical substance of the invention still fall within the scope of the technical solution of the invention. (CN114287302)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of comprehensive utilization of straw, and particularly relates to a method for harvesting rice, carbon sequestration, emission reduction, weight reduction and synergy in Jidong coastal rice areas.|BACKGROUND ART|[0002] The Jidong coastal rice area is a main rice producing area in Hebei province, and the planting area is about 100 ten thousand mu. The annual rice straw yield is about 70-80 ten thousand tons, and most of the annual rice straw yield is burnt due to the lack of efficient utilization technology, so that not only is the resource wasted and the soil ecosystem destroyed, but also the atmospheric pollution is caused. In recent years, the government has strictly prohibited straw burning and has vigorously advocated straw returning. It is known that straw returning is an effective measure for improving the organic carbon content of soil, but if returning is not reasonable, CH is greatly promoted 4 The emissions, and hence the increased greenhouse effect, will be higher than its carbon fixation effect. In the area, the temperature is low in winter and spring, and the straws return to the field for decompositionThe slow speed, especially the overlapping of the natural decomposition period of the straw and the turning green and tillering period of the rice, seriously inhibits the growth of seedlings, and becomes a main factor influencing the large-area popularization of the straw returning technology. In addition, the problems of unreasonable fertilizer proportion, low fertilizer application accuracy and the like exist in the rice planting process under the condition of returning the straw to the field, so that the fertilizer utilization rate is low, the cultivated quality is reduced, the emission of greenhouse gases is increased, and adverse effects are generated on farmlands and the ecological environment of the atmosphere. Therefore, establishing a reasonable carbon sequestration emission reduction and weight loss synergy technology is one of the urgent tasks in the current area.|DISCLOSURE|Disclosure of Invention|[0003] Aiming at the defects of the prior art, the invention provides a carbon sequestration emission reduction, weight reduction and synergy method for harvesting rice in the Jidong coastal rice area, which is characterized in that the reasonable carbon sequestration emission reduction, weight reduction and synergy method for harvesting rice in the Jidong coastal rice area is constructed by carefully analyzing the precise fertilization of released nitrogen, phosphorus and potassium in the process of straw decomposition in the returning period, the non-cultivation period, the transplanting period and the straw decomposition period, thereby not only promoting the recycling process of rice straw, reducing environmental pollution and protecting ecological environment, but also having better economic, ecological and social benefits and being beneficial to the green and sustainable development of agriculture.|[0004] In order to solve the technical problems, the invention adopts the following technical scheme: a Jidong coastal rice harvesting carbon sequestration emission reduction, weight losing and synergy method is characterized by comprising the following steps:|[0005] s1, crushing rice harvesting straws in autumn and returning the crushed straws to the field: harvesting rice in a harvester at the end of 10 months of the first year to the last ten days of 11 months, wherein the stubble height of the rice stubble is 10 cm-15 cm, crushing the straw into 5 cm-10 cm length, returning the whole amount of straw to the field to obtain returning straw, broadcasting a rice straw decomposing inoculant on the returning straw, and ploughing the rice straw decomposing inoculant, the returning straw and the rice stubble together; irrigation in the non-cultivation period to enable the soil to reach saturated water content;|[0006] the rice straw decomposing inoculant is prepared from the following raw materials in parts by weight: 20 to 50 parts of termite fungus (isoptercola sp.), 20 to 50 parts of trichoderma longibrachiatum (Trichoderma longibrachiatum), 20 to 50 parts of streptomyces fingii (Streptomyces finlayi), 20 to 50 parts of Staphylococcus (Staphylococcus sp.), 10 to 30 parts of bacillus subtilis (Bacillus subtilis) and 10 to 30 parts of bacillus mucilaginosus (Bacillus mucilaginosus);|[0007] s2, rotary tillage is carried out at the beginning of 5 months of the second year, raking is carried out in the middle of 5 months, and 450kg/hm of the rotary tillage is applied 2 ～600kg/hm 2 The slow-release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, and is subjected to sealing treatment before transplanting by using herbicide under the condition that the water layer is 5 cm-7 cm in 5-7 days before transplanting;|[0008] s3, selecting rice seedlings with the height of 10 cm-15 cm, yellow-green leaves and white roots for transplanting in the middle and late 5 months, wherein the transplanting density is 30cm multiplied by 16cm for each plant;|[0009] s4, dressing 3 times every 7 days after transplanting, wherein 97.5kg/hm is dressed 1 st time 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a);|[0010] s5, before the occurrence of rice diseases and insect pests, pesticide is sprayed for controlling.|[0011] Preferably, the non-cultivation period in S1 refers to a period from when the rice straw decomposing inoculant, the returning straw and the rice stubble are ploughed together to when the rice straw is rotary tillage.|[0012] Preferably, the returning amount of the returning straw in S1 is 18t/hm 2 ～25t/hm 2 The broadcast application amount of the rice straw decomposing inoculant is 30L/hm 2 ～45L/ hm 2 。|[0013] Preferably, the ploughing depth in the step S1 is 10 cm-15 cm.|[0014] Preferably, the mass fraction of N in the slow release fertilizer of nitrogen, phosphorus and potassium in S2 is 25%, P 2 O 5 Is 9% by mass, K 2 The mass fraction of O is 11%.|[0015] Preferably, the water layer is exposed from 50 to 60 percent of soil blocks during S2 raking.|[0016] Preferably, the herbicide in S2 is a mixture of 40% oxadiazon-pretilachlor microemulsion and 10% pyrazosulfuron-ethyl wettable powder; the mass fraction of pretilachlor in the 40% oxadiazon microemulsion is 30%, and the mass fraction of oxadiazon is 10%; the dosage of the 40% oxadiazon micro-emulsion is 90 ml/mu to 100 ml/mu; the dosage of the 10% pyrazosulfuron-ethyl wettable powder is 15 g/mu-20 g/mu.|[0017] Preferably, the method of sealing treatment before insertion in S2 adopts unmanned aerial vehicle spraying, the spraying width is 10m, the flying height is 2.5m, the flying speed is 8m/S, and the liquid medicine atomization grade is 550 microns.|[0018] Preferably, the spraying of the pesticide in S5 is:|[0019] spraying 200 g/L chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent with the dosage of 5 mL/mu in the jointing period;|[0020] spraying 20 mL/mu of 25% pyraclostrobin suspending agent, 40 g/mu of 75% tricyclazole wettable powder, 7.5 mL/mu of 200 g/liter chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent in the booting stage;|[0021] spraying 20 mL/mu of 25% pyraclostrobin suspending agent, 60 g/mu of 30% tricyclazole suspending agent and 20 g/mu of 25% pymetrozine suspending agent in the heading period;|[0022] spraying 25 mL/mu of 20% of enoxime tebuconazole suspending agent, 60 mL/mu of 30% of tricyclazole suspending agent and 20 g/mu of 25% of pymetrozine suspending agent in the period of lactation;|[0023] the mass fractions of pyraclostrobin and tebuconazole in the 25% pyraclostrobin-penconazole suspending agent are 12.5%; the mass fractions of the enestroburin and the tebuconazole in the 20% enestroburin-tebuconazole suspending agent are 10%.|[0024] Compared with the prior art, the invention has the following advantages:|[0025] the reasonable carbon fixation, emission reduction, weight reduction and synergy method for Jidong coastal rice areas is constructed through meticulous analysis of precise fertilization by releasing nitrogen, phosphorus and potassium in the returning period, the non-cultivation period moisture management, the transplanting period and the straw decomposition process, so that the recycling process of rice straw is promoted, the environmental pollution is reduced, the ecological environment is protected, better economic, ecological and social benefits are realized, and the green and sustainable development of agriculture is facilitated.|[0026] The invention is described in further detail below with reference to the drawings and examples.|DRAWINGS DESCRIPTION|[0027] Fig. 1 shows the residual straw ratios under different treatments according to example 3 of the present invention.|[0028] Fig. 2 shows temperature changes in the Cao Feidian region 2016-2020 of example 3 of the present invention.|INVENTION MODE|Detailed Description|Example 1|[0029] The test is carried out at a coastal agriculture comprehensive test station (39 DEG 17'40' 'N-118 DEG 27'22'' E) of the national academy of sciences of agriculture and forestry in Hebei province, the altitude of the test station is 2.5 meters, the test station belongs to the warm-warm zone semi-humid seasonal offshore continental climate in the eastern monsoon area, the annual average temperature is 11.4 ℃, the annual precipitation is 635.9mm, and the test station is concentrated in 7-8 months. The rice variety tested was Bindao 18.|[0030] The embodiment is a method for harvesting rice, fixing carbon, reducing emission, losing weight and enhancing efficiency in Jidong coastal rice areas, which comprises the following steps:|[0031] s1, crushing rice harvesting straws in autumn and returning the crushed straws to the field: harvesting rice by a harvester at the bottom of 10 months in the first year (10 months in 2020), wherein the stubble height of rice stubble is 10cm, crushing the straw into 5cm long, returning the whole straw to the field to obtain returning straw, spreading a rice straw rotting microbial inoculum on the returning straw, and ploughing the rice straw rotting microbial inoculum, the returning straw and the rice stubble together, wherein the ploughing depth is 10cm; irrigation in the non-cultivation period to enable the soil to reach saturated water content; the non-cultivation period refers to the period from when the rice straw decomposing inoculant, the returning straw and the rice stubble are ploughed together to when the rice straw is rotary tillage is performed; the returning amount of the returning straw is 25t/hm 2 The broadcast application amount of the rice straw returning decomposing inoculant is 45L/hm 2 ;|[0032] The rice straw returning decomposing inoculant is prepared from the following raw materials in parts by weight: 20 parts of termite fungus, 20 parts of trichoderma longibrachiatum, 20 parts of streptomyces fingii, 50 parts of staphylococcus, 30 parts of bacillus subtilis and 30 parts of bacillus mucilaginosus;|[0033] s2, rotary tillage is carried out at the beginning of 5 months (5 months and 5 days) of the second year, raking is carried out in the middle of 5 months (5 months and 12 days), and 600kg/hm of the fertilizer is applied 2 The slow-release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, a water layer is exposed at 50% soil when raking, the sealing treatment before transplanting is carried out by using herbicide under the condition that the water layer is 5cm 5 days before transplanting, unmanned aerial vehicle is adopted for spraying, the spraying width is 10m, the flying height is 2.5m, the flying speed is 8m/s, and the pesticide is preparedThe liquid atomization grade is 550 microns; the mass fraction of N in the nitrogen-phosphorus-potassium slow release fertilizer is 25%, and P is the same as that of the slow release fertilizer 2 O 5 Is 9% by mass, K 2 The mass fraction of O is 11%;|[0034] the herbicide is a mixture of 40% oxadiazon-pretilachlor microemulsion with the dosage of 90 ml/mu and 10% pyrazosulfuron-ethyl wettable powder with the dosage of 15 g/mu; the mass fraction of pretilachlor in the 40% oxadiazon microemulsion is 30%, and the mass fraction of oxadiazon is 10%;|[0035] s3, selecting rice seedlings with the height of 10 cm-15 cm and the yellow-green leaves and white roots for transplanting in the middle ten days of 5 months (19 days of 5 months), wherein the transplanting density is 30cm multiplied by 16cm for each plant area;|[0036] s4, dressing 3 times every 7 days after transplanting, wherein 97.5kg/hm is dressed 1 st time 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a);|[0037] s5, before the occurrence of rice diseases and insect pests, spraying pesticides for control, and spraying 200 g/L chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent at the jointing period;|[0038] spraying 20 mL/mu of 25% pyraclostrobin suspension, 40 g/mu of 75% tricyclazole wettable powder, 7.5 mL/mu of 200 g/liter chlorantraniliprole suspension and 20 g/mu of 25% pymetrozine suspension in the booting stage;|[0039] spraying 20 mL/mu of 25% pyraclostrobin suspension, 60 g/mu of 30% tricyclazole suspension and 20 g/mu of 25% pymetrozine suspension in the heading period;|[0040] spraying 20% of diniconazole suspending agent, 30% of tricyclazole suspending agent and 25% of pymetrozine suspending agent, wherein the concentration of diniconazole suspending agent is 25 mL/mu, the concentration of tricyclazole suspending agent is 60 mL/mu, and the concentration of pymetrozine suspending agent is 20 g/mu in the lactation period;|[0041] the mass fractions of pyraclostrobin and tebuconazole in the 25% pyraclostrobin-tebuconazole suspension are 12.5%; the mass fractions of the deoxim-methyl and the tebuconazole in the 20% deoxim-tebuconazole suspending agent are 10%.|[0042] The test adopts a single factor test and sets a comparison, CK is not returned to the field, the treatment is respectively set as T1-T3, T1 is returned to the field under the action of HT20 (the rice straw decomposing inoculant of the embodiment), and T2 isThe straw returning to the field under the action of the Nongfukang straw returning decomposition agent (commercially available from Nongfukang biotechnology Co., ltd.) and T3 is the returning to the field without the decomposition agent. Irrigation is carried out in a proper amount in a non-cultivation period, transplanting is carried out for 5 months and 21 days, and the fertilizer application scheme in the cultivation period is as follows: the CK straw is not returned to the field and is treated by conventional fertilization, T1-T3 adopts a fertilizer reducing scheme (table 1), the base fertilizer is applied once, the tiller fertilizer is applied in three times, and the first 97.5kg/hm 2 The latter two times are respectively 112.5kg/hm 2 The spike fertilizer is applied when the spike length reaches 0.3-0.5 cm. The pesticide and the water management measure are the same as the conventional method. The cell area is 744m 2 (18.6X10 m). CH was measured at 10-day intervals at tillering stage 4 And N 2 O emission, yield and soil organic matter content were measured during harvest.|[0043] TABLE 1 chemical fertilizer hypo-application scheme|[0044] |[0045] TABLE 2 yield and soil organic matter content|[0046] |[0047] Note that: the different lowercase letters in the tables indicate that the differences reach a significant level P <0.05, as in the following tables.|[0048] TABLE 3 tillering stage CH 4 And N 2 Accumulated O discharge|[0049] |[0050] After the method is applied, compared with the conventional fertilization without returning the straw to the field, not only the fertilizer application reduction is realized, but also the carbon fixation and emission reduction of the rice field, the rice yield and benefit increase (tables 2 and 3) are realized, the organic content of the soil is improved by 13.36-37.79%, and the CH at the tillering stage is improved 4 And N 2 The accumulated O discharge amount is respectively reduced by 61.86 percent and 56.67 percent; according to the price of 2.6 yuan/kg of paddy, the rice straw decomposing inoculant of the embodiment is applied to the field on the basis of 26.5% of fertilizer decrement, the yield of rice per mu is increased by 2.26%, and the cost per mu is saved by 131.12 yuan.|[0051] Example 2|[0052] The experiment was performed in 2020-2021 on four farms in Cao Feidian area of Tangshan, hebei province. Physical and chemical properties of 0-20cm plough layer soil in test field: the total salt content is 1.39 g/kg, the pH value is 7.51, the organic matter content is 18.56g/kg, and the quick-acting phosphorus content is 20.13g/kg. Quick-acting potassium 255.12 mg/kg and quick-acting nitrogen 78.81 mg/kg.|[0053] The embodiment is a method for harvesting rice, fixing carbon, reducing emission, losing weight and enhancing efficiency in Jidong coastal rice areas, which comprises the following steps:|[0054] s1, crushing rice harvesting straws in autumn and returning the crushed straws to the field: harvesting rice in the first 11 th (11 th of 2020), wherein the stubble height of the rice stubble is 15cm, crushing the straw into 8cm long, returning the whole amount of straw to the field to obtain returning straw, broadcasting a rice straw rotting microbial inoculum on the returning straw, and ploughing the rice straw rotting microbial inoculum, the returning straw and the rice stubble together, wherein the ploughing depth is 15cm; irrigation in the non-cultivation period to enable the soil to reach saturated water content; the non-cultivation period refers to the period from when the rice straw decomposing inoculant, the returning straw and the rice stubble are ploughed together to when the rice straw is rotary tillage is performed; the returning amount of the returning straw is 18t/hm 2 The broadcast application amount of the rice straw decomposing inoculant is 30L/hm 2 ;|[0055] The rice straw returning decomposing inoculant is prepared from the following raw materials in parts by weight: 50 parts of termite fungus, 50 parts of trichoderma longibrachiatum, 50 parts of streptomyces fingii, 20 parts of staphylococcus, 10 parts of bacillus subtilis and 10 parts of bacillus mucilaginosus;|[0056] s2, rotary tillage is carried out at the beginning of 5 months (5 months and 8 days) of the second year, raking is carried out in the middle of 5 months (5 months and 15 days), and 450kg/hm of the fertilizer is applied 2 The slow-release fertilizer of nitrogen, phosphorus and potassium is used as a base fertilizer, a water layer is exposed by 60% soil when raking, the sealing treatment before transplanting is carried out by using herbicide under the condition that the water layer is 7cm in 7 days before transplanting, the spraying width is 10m, the flying height is 2.5m, the flying speed is 8m/s, and the atomization level of the liquid medicine is 550 microns; the mass fraction of N in the nitrogen-phosphorus-potassium slow release fertilizer is 25%, and P is the same as that of the slow release fertilizer 2 O 5 Is 9% by mass, K 2 The mass fraction of O is 11%;|[0057] the herbicide is a mixture of 40% oxadiazon-pretilachlor microemulsion with the dosage of 100 ml/mu and 10% pyrazosulfuron-ethyl wettable powder with the dosage of 20 g/mu; the mass fraction of pretilachlor in the 40% oxadiazon microemulsion is 30%, and the mass fraction of oxadiazon is 10%;|[0058] s3, in the next ten days of 5 months (23 days of 5 months), selecting rice seedlings with the height of 10 cm-15 cm, yellow-green leaves and white roots for transplanting, wherein the transplanting density is 30cm multiplied by 16cm for each plant area;|[0059] s4, dressing 3 times every 7 days after transplanting, wherein 97.5kg/hm is dressed 1 st time 2 The urea of (2) to (3) is applied 112.5kg/hm 2 Urea of (a);|[0060] s5, before the occurrence of rice diseases and insect pests, spraying pesticides for control, and spraying 200 g/L chlorantraniliprole suspending agent and 20 g/mu of 25% pymetrozine suspending agent at the jointing period;|[0061] spraying 20 mL/mu of 25% pyraclostrobin suspension, 40 g/mu of 75% tricyclazole wettable powder, 7.5 mL/mu of 200 g/liter chlorantraniliprole suspension and 20 g/mu of 25% pymetrozine suspension in the booting stage;|[0062] spraying 20 mL/mu of 25% pyraclostrobin suspension, 60 g/mu of 30% tricyclazole suspension and 20 g/mu of 25% pymetrozine suspension in the heading period;|[0063] spraying 20% of diniconazole suspending agent, 30% of tricyclazole suspending agent and 25% of pymetrozine suspending agent, wherein the concentration of diniconazole suspending agent is 25 mL/mu, the concentration of tricyclazole suspending agent is 60 mL/mu, and the concentration of pymetrozine suspending agent is 20 g/mu in the lactation period;|[0064] the mass fractions of pyraclostrobin and tebuconazole in the 25% pyraclostrobin-tebuconazole suspension are 12.5%; the mass fractions of the deoxim-methyl and the tebuconazole in the 20% deoxim-tebuconazole suspending agent are 10%.|[0065] The average mu yield of the rice is 802 kg/mu, and the average organic matter content of the soil is 26.74g/kg.|[0066] Example 3|[0067] The embodiment is a test established for a method for harvesting rice, fixing carbon, reducing emission, losing weight and enhancing efficiency in Jidong coastal rice area:|[0068] the research area is located in an agricultural test field (N39 DEG 16 '31', E118 DEG 27 '5.14') of a coastal modern agriculture comprehensive test station in Tang Shanshi Cao Feidian area, belongs to an offshore continental climate in a warm and warm zone semi-humid season in an eastern quarter wind area, and has the climatic characteristics of sufficient illumination, concentrated precipitation, synchronous rainy and hot days, distinct dry and wet seasons and the like. The average annual temperature is 11.4 ℃, the average evaporation capacity is 1969mm, the annual precipitation is 635.9mm, and the method is mainly concentrated in 7-8 months. The soil type of the test land is paddy soil, and the physical and chemical properties of 0-20cm plough layer soil are as follows: the total salt content is 1.26 g/kg, the pH value is 7.65, the organic matter is 17.94g/kg, the total nitrogen is 1.13 g/kg, and the quick-acting phosphorus is 19.90 mg/kg. Quick-acting potassium 242.32 mg/kg and quick-acting nitrogen 73.11 mg/kg.|[0069] The area is planted with single-season rice, the test material is 18, the growth period is 170-175 days, the transplanting mode is adopted, and the transplanting density is 30 multiplied by 16cm. The 3 test decomposing agents were HT20 (rice straw decomposing inoculant in example 1: 20 parts of termite fungus, 20 parts of Trichoderma longibrachiatum, 20 parts of Streptomyces fingii, 50 parts of staphylococcus, 30 parts of bacillus subtilis and 30 parts of bacillus mucilaginosus), and the agricultural straw returning decomposing agent (commercially available, agricultural biotechnology Co., ltd., NFK for short).|[0070] Test one: non-cultivation period moisture management, returning period and transplanting period selection test|[0071] The test sets a return to field D1 after harvesting the rice and a return to field D2 after soil thawing in spring of the next year. The three-split zone test is adopted, the application conditions of returning to the field and the microbial inoculum are the main factors A, the three-split zone test comprises 4 levels, and A1 to A4 are respectively the control of returning to the field by applying HT20, returning to the field by applying NFK, returning to the field without applying the microbial inoculum and returning to the field by not applying the microbial inoculum. The water management in the non-cultivation period (the time from returning straw, microbial inoculum and rice stubble to tillage together to rotary tillage) is a side factor B, and comprises 2 levels, B1 is not irrigated, B2 is irrigated, so that the water content of soil is close to the saturation state, and the water is not irrigated in a flood mode. The transplanting period is a side factor C, and comprises 3 levels, C1 early planting (about 5 months and 15 days), C2 conventional (5 months and 22 days), C3 late planting (5 months and 29 days), and fertilizer, pesticide and water management measures in the rest cultivation period are the same as conventional measures. The main area is 166m 2 The area of the secondary region is 83m 2 The area of the re-cracking zone is 25m 2 Repeated 3 times. Plant height and basic seedling per hole are investigated on day 7 after transplanting, and hanging is carried out per cellThe method comprises the steps of 10 points are investigated, the plant height and the tillering number of each point are investigated every 7 days after the 10 points are investigated, until tillering is stopped, and the effective spike number of rice is recorded.|[0072] Results and analysis|[0073] 1. Influence of irrigation in different returning period and non-cultivation period on rice tillering and ear forming|[0074] Table 4 shows that the returning period has obvious influence on the highest tillering number, tillering speed, effective spike number and spike forming rate of rice, and the returning D1 in autumn is obviously higher than that in spring. The irrigation in the non-cultivation period has obvious influence on the highest tillering number, and the highest tillering number of the irrigation treatment B2 is higher than that of the non-irrigation treatment, but has no obvious influence on the effective spike number, the spike forming rate and the tillering speed. Therefore, in autumn, the optimal returning period is adopted, and the water can be properly irrigated in the non-cultivation period in the area with sufficient water source, so that the flood irrigation of large water is avoided.|[0075] TABLE 4 tillering and ear formation rates of Rice under different moisture management at different returning to field and non-cultivation periods|[0076] |[0077] 2. Influence of different transplanting periods on rice tillering and ear forming|[0078] The different transplanting periods have a large influence on the highest tillering number, tillering speed, effective spike number and spike forming rate (Table 5), wherein the highest tillering number is represented by C1 > C2 > C3, the tillering speed is represented by C3 > C1 > C2, the effective spike number is represented by C2 > C1 > C3, and the spike forming rate is represented by C3 > C2 > C1. Overall analysis, C2 is a more suitable transplanting period.|[0079] TABLE 5 tillering and ear formation rates of Rice at different transplanting periods|[0080] |[0081] Influence of returning to field of different microbial inoculum on rice tillering and ear forming rate|[0082] The application of different microbial inoculum to the field has great influence on the highest tillering speed, effective spike number and spike forming rate of rice (Table 6). The highest tillering speed, the effective spike number and the spike forming rate under the A1 treatment are obviously higher than those of the rest treatment, wherein the highest tillering speed is expressed as A1 & gtA 4 & gtA 2 & gtA 3, the effective spike number is expressed as A1 & gtA 2 & gtA 4 & gtA 3, and the spike forming rate is expressed as A1 & gtA 2 & gtA 4 & gtA 3. As can be seen, the effect of the microbial inoculum A1 is best.|[0083] Table 6 tillering and ear forming rates of returning rice under the action of different microbial inoculum|[0084] |[0085] In conclusion, when HT20 is applied to the field in autumn, water source sufficient areas can be supplied and irrigated appropriately after returning to the field and plowing, and then seedling transplanting is carried out in the middle and late 5 months of the next year, so that the highest tillering number, the effective spike number and the spike forming rate of the rice are improved greatly.|[0086] (II) test II: accurate fertilization scheme determination|[0087] The test is carried out at a coastal agriculture comprehensive test station (39 DEG 17'40' 'N-118 DEG 27'22'' E) of the national academy of sciences of agriculture and forestry in Hebei province, the altitude of the test station is 2.5 meters, the test station belongs to the warm and warm zone semi-humid seasonal offshore continental climate of the eastern monsoon area, the annual average temperature is 11.4 ℃, the annual precipitation is 635.9mm, and the test station is concentrated in 7-8 months.|[0088] The rice variety tested was Bindao 18. Urea (N content 46%), 45% methoprene (N content 25%, P) 2 O 5 Content 9%, K 2 O content 11%), potassium sulfate (K) 2 50% of O content), 50% of silicon grain slow release fertilizer (25% of N content, P) 2 O 5 10% of K 2 O content 15%).|[0089] Transplanting at 11 months 2020, 21 months 2021 and 10 months 2021. The previous crop is rice, and HT20 (20 parts of termite fungus, 20 parts of trichoderma longibrachiatum, 20 parts of streptomyces finelegans, 50 parts of staphylococcus, 30 parts of bacillus subtilis and 30 parts of bacillus mucilaginosus) is sprayed on the straw in the harvesting season, and then the cultivation returning treatment is carried out, wherein the cultivation returning depth is 10-15cm, and the water content of the soil is nearly saturated by irrigation.|[0090] The test sets 4 treatments of conventional fertilization and decrement fertilization (see table 7 for details), the conventional fertilization T1 mainly simulates the habit fertilization of farmers; reducing fertilizer T2, reducing fertilizer 17.42%, reducing nitrogen fertilizer 6.45%; reducing fertilizer T3, reducing fertilizer 26.51%, reducing nitrogen fertilizer 20.28%; the fertilizer is reduced by T4, 34.90 percent and 26.09 percent. Each treatment was repeated 3 times and randomly arranged. The field management is consistent with the conventional management.|[0091] Table 7 fertilization scheme|[0092] |[0093] Results and analysis|[0094] 1. Rice yield constitution factor|[0095] Under the condition of returning the straw to the field, the influence of different fertilization measures on the rice yield constituent factors is shown in table 8, and significant differences exist among the yield constituent factors of each treatment group. The effective spike number of the T3 treatment group is 16.11, which is higher than that of the other three treatment groups, and is respectively improved by 8.19 percent, 12.89 percent and 9.93 percent compared with the T1, the T2 and the T4, and is obviously higher than that of the T2 treatment group. The setting rate of the T3 treatment group is 94.72%, which is obviously higher than that of the conventional fertilization T1 treatment group, and is improved by 1.23% compared with T1, and the setting rates of T2 and T4 are respectively 94.14% and 94.52%, which are not obviously different from the other three groups. The spike grain number of the T2 treatment group is significantly higher than that of the other three treatment groups, namely 339.12, and is respectively 10.5%, 3.7% and 5.6% higher than that of the other three treatment groups. The T3 treatment group had higher effective spike number and higher seed setting than the other three treatment groups. The thousand grain weights of four different treated rice plants are not significantly different and all are about 32 g.|[0096] TABLE 8 influence of different fertilization treatments on Rice composition factors under straw returning|[0097] |[0098] 2. Influence on the yield of rice|[0099] Under the condition of returning straw to field, the rice yield of the conventional fertilization T1 treatment group is 9353 kg/hm 2 The final yield of the rice in the three treatment groups of decrement fertilization T2, T3 and T4 is higher than that of the rice in the conventional fertilization T1 treatment group, which are 9951 kg/hm respectively 2 、10953 kg/hm 2 、10110 kg/hm 2 The yield is increased by 6.39%, 17.11% and 8.09% respectively. The yield increasing effect of the deweighting T3 treatment group is most remarkable and is higher than that of the deweighting T2 and T4 treatment groups.|[0100] (III) test III: research on decomposition law of straw after returning to field|[0101] The potting test is carried out at a coastal agricultural comprehensive test station (39 DEG 17'40' N-118 DEG 27'22' E) of the national academy of sciences of agriculture and forestry in Hebei province, the altitude of the test station is 2.5 meters, the potting test belongs to the warm and warm zone semi-humid seasonal offshore continental climate of the eastern monsoon area, the annual average temperature is 11.4 ℃, the annual precipitation is 635.9mm, and the potting test is concentrated in 7-8 months. The soil type is salinized coastal clay loam, and rice is planted for many years.|[0102] The rice variety is 18, the growth period is 170 days, and the rice is bred by the coastal agricultural institute of the national academy of sciences of agriculture and forestry in Hebei province. The rice straw is a local non-diseased rice straw containing 0.68% of nitrogen (N) and 0.68% of phosphorus (P) 2 O 5 ) 0.13% and potassium (K) 2 O) 1.34%, C/N67, and crushing rice straw into about 5cm by a crusher. The decomposing inoculants were HT20 (rice straw returning decomposing inoculants in example 1: termite fungus 20 parts, trichoderma longibrachiatum 20 parts, streptomyces fenti 20 parts, staphylococcus 50 parts, bacillus subtilis 30 parts, and Bacillus mucilaginosus 30 parts) and Fukan straw returning decomposing inoculants (commercially available), respectively.|[0103] Adopting a random granule design, setting 3 treatment groups which are respectively:|[0104] (1) Returning the straw to the field directly-CK;|[0105] (2) Straw also Tian Peishui rice straw the rice straw returning to field decomposing inoculant (HT 20) -JH of example 1;|[0106] (3) The straw returning is matched with a Shi Nong Fukang straw returning decomposing agent-JF;|[0107] in order to simulate field production environment, potting test micro-areas are established, each micro-area has the specification of 600cm (length) x 200cm (width) x 60cm (depth), a plastic bucket (specification of 56 x 58 cm) is filled, holes are punched at the periphery and bottom of the bucket to ensure ventilation of soil and outflow of water, gaps between the buckets are filled with soil, and each treatment is arranged in one micro-area to prevent the micro-areas from being mutually connectedPollution, reduced test error, 3 micro-areas are 3 times repeated. The test used a nylon mesh bag landfill method, the nylon mesh bag specification was length x width=50 cm x 45cm, and the aperture was 0.178mm to isolate soil. 262g (10500 kg/hm of rice straw in each bag 2 And (5) returning the total amount of the straw to the field). Each treatment is applied to soil deep ploughing in the 11 th month and 25 th 2019, and rice seedlings are transplanted in the 5 th month and 28 th 2020, 5 holes are formed in each pot, and 5 plants are planted in each hole. Production management of weeding, irrigation, plant diseases and insect pests and the like is carried out according to local habits. The rice was harvested at 10 months and 10 days 2020.|[0108] Straw samples were collected 180, 210, 225, 240, 255, 265 and 295 days after returning to the field, respectively, 7 sampling times were positive to the rice transplanting period (28 days in 5 months in 2020), the tillering period (15 days in 6 months in 2020), the jointing period (28 days in 6 months in 2020), the booting period (25 days in 7 months in 2020), the heading period (5 days in 8 months in 2020), the milk ripening period (20 days in 8 months in 2020), and the maturing period (8 days in 10 months in 2020). And 5 pots are taken each time, the straw decomposition samples are dried to constant weight at 65 ℃, and the residual rate of the rice straw is calculated. The mass residual rate and the nutrient residual rate are calculated according to the following formulas:|[0109] mass residual rate (%) =m t /M 0 ,|[0110] M in the formula 0 The initial mass of the straw before decomposition;|[0111] M t is the residual mass of the decomposed straw at t.|[0112] Results and analysis|[0113] The quality residual rate of each treated straw is reduced along with the prolongation of the decomposition time, and the straw has the characteristics of quick decomposition in the early stage and gradual and slow decomposition in the later stage, and the difference exists between different treatments (figure 1). As can be seen, the treatment with HT20 (the rice straw returning to field decomposing inoculant comprises 20 parts of termite fungus, 20 parts of trichoderma longibrachiatum, 20 parts of streptomyces finyi, 50 parts of staphylococcus, 30 parts of bacillus subtilis and 30 parts of bacillus mucilaginosus) is within 0-180 days, the mass residual rate is rapidly reduced, the rapid decomposition period is 180-225 days, the slow decomposition period is 225-295 days, the mass residual rate is basically unchanged, and the decomposition stagnation period is reached. The control treatment belongs to the fast decomposition period within 0-240 days, the slow decomposition period is 240-255 days, and the slow decomposition period is 255-295 days. The treatment of the agricultural Fukang straw returning decomposing inoculant is carried out in a rapid decomposition period within 0-225 days, a slow decomposition period within 225-240 days and a slow decomposition period within 240-295 days. Therefore, the application of the rice straw returning and decomposing inoculant for returning the rice straw to the field can accelerate the decomposition of the returning straw, the quick decomposition period of the straw is finished before transplanting, the straw enters the slow decomposition period after transplanting, the harm of a large amount of harmful gases generated by the quick decomposition to rice seedlings is reduced, and compared with the control and other decomposing inoculants, the straw returning and decomposing inoculant for returning the rice straw to the field can enter the slow decomposition period 45-60 days in advance.|[0114] As can be seen from fig. 2, the temperature change in the area Cao Feidian in 2016-2020, combined with the residual rate of the straw in different treatments, can be known that HT20 returning treatment is performed in autumn, the average temperature during returning is 6.14 ℃ within 180 days after returning, that is, the period of time is 5 months after returning, and the rest of treatment is performed within 225-240 days after returning, that is, the period of time is 7-8 months, the average temperature is 12.65 ℃, so that HT20 can be started at a lower temperature (about 6 ℃) and straw decomposition is accelerated by microbial activity. The autumn returning is better than the spring returning, from the temperature of Cao Feidian in recent years, the average temperature of 11 months is below 5.5 ℃, the average temperature of 12-1 month is above zero, the average temperature of 2 months begins to rise to above zero, the average temperature of 3 months is 7 ℃, if the rice is harvested and the HT20 returning is carried out after about 11 months, the temperature is about 5 ℃, microorganisms can be started, a certain promotion effect on straw decomposition is achieved, then the microorganisms are frozen and thawed after three months, the temperature rises to 3 months, the microorganisms start to move again, and on the basis of decomposition before sealing, the straw starts to accelerate decomposition, and compared with the spring returning, the autumn returning is more beneficial to the spring returning.|[0115] The above description is only of the preferred embodiments of the present invention, and is not intended to limit the present invention. Any simple modification, variation and equivalent variation of the above embodiments according to the technical substance of the invention still fall within the scope of the technical solution of the invention. Family Number|(99514297)|99514297|Abstract|(CN114287302B B)|The invention provides a method for carbon sequestration , emission reduction , weight loss and synergy of machine - harvested rice in a coastal rice area of East Hebei Province , which comprises the following steps : harvesting rice by using a harvester from the end of October to the first ten days of November , crushing straws , putting the crushed straws in situ , spreading a rice straw decomposing inoculant , and turning over ; irrigating in a non - cultivation period until the soil saturation water content is reached ; rotary tillage is conducted at the beginning of May in the second year , harrowing is conducted in the middle ten days of May , 450-600 kg / hm < 2 > of nitrogen - phosphorus - potassium slow - release fertilizer is applied to serve as base fertilizer , and sealing treatment is conducted 5-7 days before rice transplanting ; transplanting is conducted in mid - to - late May , topdressing is conducted three times after transplanting , 97.5 kg / hm < 2 > of urea is topdressed for the first time , and 112.5 kg / hm < 2 > of urea is topdressed for the second time to the third time ; and spraying pesticides for prevention and treatment before diseases and insect pests occur . According to the method , the resource utilization process of the rice straw is promoted , environmental pollution is reduced , the ecological environment is protected , good economic , ecological and social benefits are achieved , and green and sustainable development of agriculture is facilitated . |IPC codes|(CN114287302B B)|A01B - 079/00 |A01B - 079/02 |A01G - 022/22 |Title|(CN114287302B B)|Jidong coastal rice area machine - harvested rice carbon sequestration emission reduction , weight losing and synergy method |(CN114287302 A)|Method for carbon sequestration , emission reduction , weight loss and efficiency improvement of machine - harvested rice in coastal rice area of eastern Hebei province | Other special machines A01B-079/00|A01B-079/02|A01G-022/22 A01B-079/00|A01B-079/02|A01G-022/22 CN115191303 CN115191303 102170837 WHO=Examiner SELF=N CAT=A CN112625982|CN111512914|CN103749146|US20120222350|JP2000014257 CN112625982 93535710 WHO=Examiner SELF=Y CAT=Y|CN111512914 90122689 WHO=Examiner SELF=Y CAT=Y|CN103749146 65331242 WHO=Examiner SELF=N CAT=A|US20120222350 7204097 WHO=Examiner SELF=N CAT=A|JP2000014257 31071574 WHO=Examiner SELF=N CAT=A JP2000014257; US20120222350; CN103749146; CN111512914; CN112625982 GRANTED (CN114287302)|GRANTED ALIVE (CN114287302)|ALIVE (CN114287302)|LEGAL DETAILS FOR CN114287302|Actual or expected expiration date=2042-01-06|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-01-06|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210008061|Application date=2022-01-06|Standardized application number=2022CN-0008061|Event publication date=2022-04-08|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114287302|Publication stage code=A|Publication date=2022-04-08|Standardized publication number=CN114287302|Event publication date=2022-04-08|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-04-26|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-05-30|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN114287302|Publication stage code=B|Publication date=2023-05-30|Standardized publication number=CN114287302B|Event publication date=2023-05-30|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN114287302)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSnMzqn/ns7qhj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067980324&ekey=2084&xpn=CN114287302B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=SqhjaSuxs9OvfoeLl%252BhsFbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN114287302)|CN|(CN114287302)|CN (CN114287302)|NAME=BINHAI INSTITUTE OF AGRICULTURE HEBEI ACADEMY OF AGRICULTURE & FORESTRY SCIENCES , COUNTRY=CN|(CN114287302)|NAME=BINHAI INSTITUTE OF AGRICULTURE HEBEI ACADEMY OF AGRICULTURE & FORESTRY SCIENCES , COUNTRY=CN (CN114287302)|NAME=ZHANG WEIHUA;XI'AN HUIEN INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61244|(CN114287302)|NAME=ZHANG WEIHUA;XI'AN HUIEN INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61244 (CN114287302)|NAME=LIU YAHUI|NAME=SUN JIANPING|NAME=ZHAO ZIJING|NAME=DAI XIANGLIN|NAME=DING FENGJIE|NAME=ZHANG WEI|(CN114287302)|NAME=LIU YAHUI|NAME=SUN JIANPING|NAME=ZHAO ZIJING|NAME=DAI XIANGLIN|NAME=DING FENGJIE|NAME=ZHANG WEI 0 1 Titre: (CN114287302)|Jidong coastal rice area machine-harvested rice carbon sequestration emission reduction, weight losing and synergy method Résumé: (CN114287302)|The invention provides a method for carbon sequestration, emission reduction, weight loss and synergy of machine-harvested rice in a coastal rice area of East Hebei Province, which comprises the following steps: harvesting rice by using a harvester from the end of October to the first ten days of November, crushing straws, putting the crushed straws in situ, spreading a rice straw decomposing inoculant, and turning over; irrigating in a non-cultivation period until the soil saturation water content is reached; rotary tillage is conducted at the beginning of May in the second year, harrowing is conducted in the middle ten days of May, 450-600 kg/hm < 2 > of nitrogen-phosphorus-potassium slow-release fertilizer is applied to serve as base fertilizer, and sealing treatment is conducted 5-7 days before rice transplanting; transplanting is conducted in mid-to-late May, topdressing is conducted three times after transplanting, 97.5 kg/hm < 2 > of urea is topdressed for the first time, and 112.5 kg/hm < 2 > of urea is topdressed for the second time to the third time; and spraying pesticides for prevention and treatment before diseases and insect pests occur. According to the method, the resource utilization process of the rice straw is promoted, environmental pollution is reduced, the ecological environment is protected, good economic, ecological and social benefits are achieved, and green and sustainable development of agriculture is facilitated. 45 Abstract gpt-4o-mini no The article focuses on agricultural practices for carbon sequestration related to rice cultivation, without addressing mineral weathering or CO₂ capture through enhanced weathering processes.
46 CN202111162973 CN202111162973 CN113786806 97651204 CN113786806 A 2021-12-14 [CN113786806] 2021-09-30 2021-09-30 2021-12-14 (CN113786806)|2024-09-13 (CN113786806)|Ternary modified sludge carbon fluorine removal agent and preparation method thereof (CN113786806)|The invention discloses a ternary modified sludge carbon fluorine removal agent and a preparation method thereof. The preparation method comprises the following steps: pyrolyzing dried sludge powder for 60-90 min at a temperature of 650-700 DEG C so as to obtain sludge biochar; mixing the sludge biochar with potassium acetate according to a mass ratio of 1: (2-2.5), then conducting pyrolyzing at 650-700 DEG C for 60-90 minutes, and successively performing centrifuging, washing, drying and crushing to obtain sludge-based biochar; dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the biochar prepared in the step 2; dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7-7.5, conducting full stirring for 12-14 hours, and successively performing centrifuging, washing, drying and crushing to obtain the ternary modified sludge carbon fluorine removal agent. According to the ternary modified sludge carbon fluorine removal agent, the removal rate of fluoride with 20 mg/L reaches 95% or above, adsorption capacity is 80-100 mg/g, and a water environment adaptive pH range is 2-11. NANTONG UNIVERSITY (CN113786806)|NANTONG UNIVERSITY ([CN]) YE ZHANGQING|LI SHUSHU|SONG MINGSHAN|ZHOU QINGWEN (CN113786806)|YE ZHANGQING|LI SHUSHU|SONG MINGSHAN|ZHOU QINGWEN (CN113786806)|QIAN CHAO;NANJING JINGWEI PATENT & TRADEMARK AGENCY CO., LTD|Reg. Nb: 32200 (CN113786806)|The early construction cost and the floor space are greatly saved, and the later operation is greatly saved, but the prior art is slightly insufficient considering that the generated fine particles are difficult to precipitate and easy to be polluted by a membrane, and the pH value of the treated water is lower.| (CN113786806)|1. A preparation method of a ternary modified sludge carbon defluorinating agent is characterized by comprising the following steps: the preparation method comprises the following specific steps:the first step is as follows: pyrolyzing the dried sludge powder at 650-700 ℃ for 60-90min to obtain sludge biochar;secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2-2.5, then pyrolyzing the mixture for 60-90min at the temperature of 650-700 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar;dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the sludge-based biochar prepared in the step 2;and fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7-7.5, fully stirring for 12-14 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge carbon defluorinating agent.| (CN113786806)|The application also discloses the ternary modified sludge carbon defluorinating agent prepared by the preparation method.|The application discloses a ternary modified sludge carbon fluorine removal agent and a preparation method thereof, wherein dried sludge powder is pyrolyzed at 650-700 ℃ for 60-90min to obtain sludge biochar; mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2-2.5, then pyrolyzing for 60-90min at 650-700 ℃, centrifuging, washing, drying and crushing to obtain sludge-based biochar; dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the biochar prepared in the step 2; then dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7-7.5, fully stirring for 12-14 hours, centrifuging, washing, drying and crushing to obtain a ternary modified sludge coal defluorinating agent; the removal rate of 20mg/L fluoride reaches more than 95%, the adsorption capacity is 80-100 mg/g, and the water environment adaptive pH range is 2-11.|in order to achieve the purpose, the application is realized by the following technical scheme:| (CN113786806)|SLUDGE BIOCHAR(100,27)|SLUDGE CARBON DEFLUORINATING(100,6)|SEWAGE PEAT DEFLUORINATING(100,5)|SOIL PEAT DEFLUORINATING(96,4)|TERNARY MODIFIER HYDROFLUORIC(78,5)|TERNARY MODIFIER(67,18)|SLUDGE COAL DEFLUORINATING(58,4)|SLUDGE CARBON FLUORINE(45,5)|SLUDGE CARBON FLUORINE REMOVAL(39,5)|SLUDGE POWDER(36,1)|CENTRIFUGATION(33,13)|HYDROFLUORIC POTASSIUM ACETATE(29,6)|SLUDGE DRYING POWDER(25,5)|TREATED SLUDGE BIOCHAR(25,3)|ADSORPTION CAPACITY(22,4)|SLUDGE(21,8)|DISSOLVING ALUMINUM CHLORIDE(21,6)|CERIUM CHLORIDE(17,11)|FERRIC CHLORIDE(16,11)|MIXED SOLUTION(16,6)|SODIUM HYDROXIDE SOLUTION(15,11)|BIOCHAR(15,6)|EARLY CONSTRUCTION COST(15,1)|SODIUM HYDROXIDE(14,11)|POTASSIUM ACETATE(14,7)|ENVIRONMENT ADAPTIVE PH RANGE(14,2)|WATER TREATMENT(13,1)|FLUORIDE(12,6)|FINE PARTICLE GENERATION(12,1)|SLUDGE BIOCHAR PORE CANAL(12,1)|ALUMINUM CHLORIDE(11,11)|DROPWISE(11,5)|ETHYLENEDIAMINE(11,3)|SYNTHESIZING(10,10)|DEIONIZED WATER(10,6)|LANTHANUM CHLORIDE HYDRATE(10,6)|CHITOSAN(10,3)|LATE OPERATION(10,1)|DISODIUM HYDROGEN PHOSPHATE(9,6)|MASS RATIO(8,6)|FLOOR SPACE(8,1)|LIGHT MAGNESIUM OXIDE(7,6)|BIOCHAR MASS VOLUME RATIO(7,4)|FLUORINE CONTAMINATION(7,3)|ADSORPTION DEFLUORINATION(7,1)|FERROUS METALLURGY INDUSTRY(7,1)|FLUORINE ION(5,2)|VACUUM DRYING(5,2)|FLOCCULATION PRECIPITATION(5,1)|FLUORIDE ADSORBENT(5,1)|SLUDGE DESTINATION(5,1)|FERRIC CHLORIDE MOLAR RATIO(4,3)|VOLUME RATIO MASS(4,3)|REMOVING FLUORINE(4,2)|ALUMINUM ELECTROLYSIS(4,1)|BIOCHAR PORE DIAMETER(4,1)|BONE HEALTH(4,1)|DEFLUORINATING(4,1)|HARMFUL SUBSTANCE(4,1)|SYNERGISTIC INTERACTION(4,1)|URANIUM SEPARATION(4,1)|COMPARED HYDROFLUORIC(3,2)|ADSORPTION PERFORMANCE(3,1)|COMPOSITE RARE EARTH PERFORMANCE(3,1)|EQUIVALENT SUBSTITUTION(3,1)|FLUORINE PHILIC COMPLEX(3,1)|INDUSTRIALIZATION(3,1)|400 MESH SIEVE(2,1)|ABSORBANCE(2,1)|ALKALINITY(2,1)|BIOMASS(2,1)|DENTAL FLUOROSIS(2,1)|DEVELOPING COUNTRY(2,1)|DISSOLUTION(2,1)| (CN113786806)|1. A preparation method of a ternary modified sludge carbon defluorinating agent is characterized by comprising the following steps: the preparation method comprises the following specific steps:|the first step is as follows: pyrolyzing the dried sludge powder at 650-700 ℃ for 60-90min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2-2.5, then pyrolyzing the mixture for 60-90min at the temperature of 650-700 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar;|dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the sludge-based biochar prepared in the step 2;|and fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7-7.5, fully stirring for 12-14 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge carbon defluorinating agent.|2. The method for preparing the ternary modified soil peat defluorinating agent according to claim 1, which is characterized in that: the aluminum chloride in the third step: cerium chloride: the molar ratio of the ferric chloride is 2:1: 0.01-0.05.|3. The method for preparing the ternary modified soil peat defluorinating agent according to claim 1, which is characterized in that: and in the third step, the mass-volume ratio of the biochar to the ternary modifier is 1-2g:50 mL.|4. The preparation method of the ternary modified sludge carbon fluorine removal agent according to claim 3, which is characterized in that: before the sludge-based biochar is mixed with the ternary modifier in the third step, 100 parts of sludge-based biochar, 1-5 parts of lanthanum chloride hydrate, 3-7 parts of disodium hydrogen phosphate, 2-6 parts of chitosan, 3-5 parts of light magnesium oxide and 1-3 parts of ethylenediamine are weighed according to the mass part ratio, ultrasonically dispersed for 2 hours, centrifuged at 3000rpm, ground after vacuum drying, sieved by a 200-mesh and 400-mesh sieve to treat the sludge-based biochar, and then the ternary modifier is added according to the mass volume ratio of the treated sludge-based biochar to the ternary modifier of 1-2g:50 mL.|5. The method for preparing the ternary modified soil peat defluorinating agent according to claim 1, which is characterized in that: the concentration of the sodium hydroxide solution in the fourth step is 1-3 mol/L.|6. The method for preparing the ternary modified soil peat defluorinating agent according to claim 1, which is characterized in that: the temperature of the drying in the second step and the fourth step is 60-90 ℃.|7. The ternary modified sludge carbon fluorine removal agent prepared by the preparation method of any one of claims 1 to 6. (CN113786806)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of removal of fluoride in wastewater, and particularly relates to a ternary modified sludge carbon fluorine removal agent and a preparation method thereof.|BACKGROUND ART|[0002] Fluorine contamination remains a worldwide problem, particularly in developing countries such as china, india, south africa, bangladesh, and the like. The fluorine pollution is mainly caused by a large amount of fluoride produced in industrialization and urbanization, such as metallurgy industries of ferrous metallurgy, aluminum electrolysis, lead-zinc smelting, copper smelting, rare earth separation, uranium separation, photovoltaic industry, lithium ion batteries and the like, and the fluoride in the industrial wastewater containing high fluorine can permeate into underground water and be absorbed by soil to form fluorine pollution in peripheral areas. According to statistics, 3 hundred million people worldwide drink water with fluoride concentration over 1.5mg/L, while the fluorine ion concentration in the Chinese drinking water standard can not exceed 1.0mg/L, and the fluorine ion concentration in the factory discharge wastewater can not exceed 10 mg/L. Fluoride is often essential for mineralization of human tissues, such as maintenance of bone health and enamel formation, but drinking water containing high concentrations of fluoride for extended periods of time can have deleterious effects on the human body, leading to fluorosis, such as dental fluorosis, and even retardation of growth and development in children.|[0003] The biochar serving as a good fluoride adsorbent is wide in source, the organic matter content of the sludge is generally 33.5-47.2%, and the biochar contains rich organic matters such as protein and lipid, so that the biochar can be prepared into a porous material with an oxidation functional group and an aromatic surface by pyrolyzing and carbonizing the sludge like other biomass.|[0004] Chinese patent CN201910070431.8 discloses a wastewater high-efficiency fluorine removal agent and a preparation method thereof. Is prepared by combining various rare earth metal salts with inorganic metal salts. The rare earth metal salt forms hydroxylation under certain conditions, is dispersed under the combined action of various metal salts to form a fluorine-philic complex, forms floccules under the action of a flocculating agent, and is directly precipitated, so that the defluorination effect is achieved, the advantages of chemical precipitation, flocculation precipitation and adsorption defluorination technologies are taken into consideration, calcium salt does not need to be additionally added, and flocculating agent and adsorbent do not need to be additionally added. The effects of removing fluorine, ss and other harmful substances can be met only by one set of integrated wastewater treatment equipment. The early construction cost and the floor space are greatly saved, and the later operation is greatly saved, but the prior art is slightly insufficient considering that the generated fine particles are difficult to precipitate and easy to be polluted by a membrane, and the pH value of the treated water is lower.|DISCLOSURE|Disclosure of Invention|[0006] The technical problem to be solved is as follows:|aiming at the defects of the prior art, the method solves the problems that the existing cost is higher, and the existing method is not suitable for the wastewater containing solid particles with high salinity and complete dissolution; provides a ternary modified sludge carbon fluorine removal agent and a preparation method thereof.|[0007] The technical scheme is as follows:|in order to achieve the purpose, the application is realized by the following technical scheme:|a ternary modified sewage peat defluorinating agent and a preparation method thereof are disclosed, wherein the preparation method comprises the following specific steps:|the first step is as follows: pyrolyzing the dried sludge powder at 650-700 ℃ for 60-90min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2-2.5, then pyrolyzing the mixture for 60-90min at the temperature of 650-700 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar;|dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the sludge-based biochar prepared in the step 2;|and fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7-7.5, fully stirring for 12-14 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge carbon defluorinating agent.|[0008] As a preferred technical scheme of the invention: the aluminum chloride in the third step: cerium chloride: the molar ratio of the ferric chloride is 2:1: 0.01-0.05.|[0009] As a preferred technical scheme of the invention: and in the third step, the mass-volume ratio of the biochar to the ternary modifier is 1-2g:50 mL.|[0010] As a preferred technical scheme of the invention: before the sludge-based biochar is mixed with the ternary modifier in the third step, 100 parts of sludge-based biochar, 1-5 parts of lanthanum chloride hydrate, 3-7 parts of disodium hydrogen phosphate, 2-6 parts of chitosan, 3-5 parts of light magnesium oxide and 1-3 parts of ethylenediamine are weighed according to the mass part ratio, ultrasonically dispersed for 2 hours, centrifuged at 3000rpm, ground after vacuum drying, sieved by a 200-mesh and 400-mesh sieve to treat the sludge-based biochar, and then the ternary modifier is added according to the mass volume ratio of the treated sludge-based biochar to the ternary modifier of 1-2g:50 mL.|[0011] As a preferred technical scheme of the invention: the concentration of the sodium hydroxide solution in the fourth step is 1-3 mol/L.|[0012] As a preferred technical scheme of the invention: the temperature of the drying in the second step and the fourth step is 60-90 ℃.|[0013] The application also discloses the ternary modified sludge carbon defluorinating agent prepared by the preparation method.|[0014] Has the advantages that:|the application provides a ternary modified sludge carbon defluorinating agent and a preparation method thereof, and compared with the prior art, the ternary modified sludge carbon defluorinating agent has the following beneficial effects:|1. the method provides a new way for the destination of the sludge, so that the sludge becomes an economic and feasible material which is not influenced by seasons, and the method can be widely applied to the removal of fluoride in a water environment;|2. the prepared defluorination material has good adsorption performance, large adsorption capacity and rich and environment-friendly raw materials.|[0015] 3. Compared with the prior art, the invention further enlarges the pore volume and the pore diameter of the biochar through the potassium acetate, thereby better loading the metal composite component in the pore canal of the sludge-based biochar and finally synthesizing the biological defluorinating agent with high adsorption efficiency.|[0016] 4. The specific surface area of the biochar is enlarged by adopting a specific preparation process, oxygen-containing functional groups and metal oxides are introduced, and the components interact with each other, so that a better synergistic effect is exerted.|[0017] 5. The sludge-based biological adsorption material improves the performance of the composite rare earth high-polymer aluminum-based fluorine agent, and can widen the application range to alkalinity reaching 2-11.|[0018] 6. Under the action of oxygen-containing functional groups and metal ions on the surface of the biochar, the components have better synergistic interaction, the pH range of adsorption is widened, and the method can be better applied to removal of fluoride in wastewater.|[0019] 7. The removal rate of 20mg/L fluoride reaches more than 95%, the adsorption capacity is 80-100 mg/g, and the water environment adaptive pH range is 2-11.|[0020] 8. The cost is low; the adsorption capacity is greatly improved; the application range is greatly widened.|DRAWINGS DESCRIPTION|[0021] Description of the drawings:|FIG. 1 is a graph showing the absorbance of the present application at various pH values at an initial concentration of 20 mg/L.|[0022] FIG. 2 is a graph of absorbance of the present application at various initial concentrations at an initial pH of 6.|INVENTION MODE|Detailed Description|[0024] The following will further explain the embodiments and working procedures of the present invention by referring to examples.|[0025] Example 1:|a ternary modified sewage peat defluorinating agent and a preparation method thereof, the steps are as follows:|the first step is as follows: pyrolyzing the dried sludge powder at 700 ℃ for 90min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2.5, then pyrolyzing the mixture for 90min at 700 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar; the drying temperature is 90 ℃;|dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier; weighing 100 parts of sludge-based biochar, 1-5 parts of lanthanum chloride hydrate, 3-7 parts of disodium hydrogen phosphate, 2-6 parts of chitosan, 3-5 parts of light magnesium oxide and 1-3 parts of ethylenediamine according to the mass part ratio, performing ultrasonic dispersion for 2 hours, centrifuging at the speed of 3000rpm, drying in vacuum, grinding, treating the sludge-based biochar through a 200-mesh and 400-mesh sieve, and then adding a ternary modifier into the sludge-based biochar according to the mass volume ratio of the treated sludge-based biochar to the ternary modifier of 2g:50mL to fully mix the sludge-based biochar; the aluminum chloride in the third step: cerium chloride: the molar ratio of ferric chloride is 2:1: 0.05;|fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7.5, fully stirring for 14 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge coal defluorinating agent; the concentration of the sodium hydroxide solution in the fourth step is 3 mol/L; the temperature of drying was 90 ℃.|[0026] Example 2:|a ternary modified sewage peat defluorinating agent and a preparation method thereof, the steps are as follows:|the first step is as follows: pyrolyzing the dried sludge powder at 680 ℃ for 70min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2.2, then pyrolyzing the mixture for 70min at 680 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar; the drying temperature is 70 ℃;|thirdly, dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the biochar prepared in the step 2; the aluminum chloride in the third step: cerium chloride: the molar ratio of ferric chloride is 2:1: 0.03; in the third step, the mass-volume ratio of the biochar to the ternary modifier is.5 g:50 mL;|fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7.3, fully stirring for 13 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge coal defluorinating agent; the concentration of the sodium hydroxide solution in the fourth step is 2 mol/L; the temperature of drying was 70 ℃.|[0027] Example 3:|a ternary modified sewage peat defluorinating agent and a preparation method thereof, the steps are as follows:|the first step is as follows: pyrolyzing the dried sludge powder at 650 ℃ for 60min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2, then pyrolyzing the mixture for 60min at 650 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar; the drying temperature is 60 ℃;|thirdly, dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the biochar prepared in the step 2; the aluminum chloride in the third step: cerium chloride: the molar ratio of ferric chloride is 2:1: 0.01; in the third step, the mass-volume ratio of the biochar to the ternary modifier is 1g:50 mL;|fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7, fully stirring for 12 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge coal defluorinating agent; the concentration of the sodium hydroxide solution in the fourth step is 1 mol/L; the temperature of drying was 60 ℃.|[0028] The parameters of pyrolysis temperature, activation temperature, alkali concentration, metal ion proportion, stirring time and the like are controlled within a set range, different products are obtained, and the adsorption capacity of the products is changed between 80 and 100 mg/g.|[0029] Finally, the above embodiments are only for illustrating the technical solutions of the present invention and not for limiting, and other modifications or equivalent substitutions made by the technical solutions of the present invention by the person skilled in the art shall be covered by the scope of the claims of the present invention without departing from the spirit and scope of the technical solutions of the present invention. (CN113786806)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of removal of fluoride in wastewater, and particularly relates to a ternary modified sludge carbon fluorine removal agent and a preparation method thereof.|BACKGROUND ART|[0002] Fluorine contamination remains a worldwide problem, particularly in developing countries such as china, india, south africa, bangladesh, and the like. The fluorine pollution is mainly caused by a large amount of fluoride produced in industrialization and urbanization, such as metallurgy industries of ferrous metallurgy, aluminum electrolysis, lead-zinc smelting, copper smelting, rare earth separation, uranium separation, photovoltaic industry, lithium ion batteries and the like, and the fluoride in the industrial wastewater containing high fluorine can permeate into underground water and be absorbed by soil to form fluorine pollution in peripheral areas. According to statistics, 3 hundred million people worldwide drink water with fluoride concentration over 1.5mg/L, while the fluorine ion concentration in the Chinese drinking water standard can not exceed 1.0mg/L, and the fluorine ion concentration in the factory discharge wastewater can not exceed 10 mg/L. Fluoride is often essential for mineralization of human tissues, such as maintenance of bone health and enamel formation, but drinking water containing high concentrations of fluoride for extended periods of time can have deleterious effects on the human body, leading to fluorosis, such as dental fluorosis, and even retardation of growth and development in children.|[0003] The biochar serving as a good fluoride adsorbent is wide in source, the organic matter content of the sludge is generally 33.5-47.2%, and the biochar contains rich organic matters such as protein and lipid, so that the biochar can be prepared into a porous material with an oxidation functional group and an aromatic surface by pyrolyzing and carbonizing the sludge like other biomass.|[0004] Chinese patent CN201910070431.8 discloses a wastewater high-efficiency fluorine removal agent and a preparation method thereof. Is prepared by combining various rare earth metal salts with inorganic metal salts. The rare earth metal salt forms hydroxylation under certain conditions, is dispersed under the combined action of various metal salts to form a fluorine-philic complex, forms floccules under the action of a flocculating agent, and is directly precipitated, so that the defluorination effect is achieved, the advantages of chemical precipitation, flocculation precipitation and adsorption defluorination technologies are taken into consideration, calcium salt does not need to be additionally added, and flocculating agent and adsorbent do not need to be additionally added. The effects of removing fluorine, ss and other harmful substances can be met only by one set of integrated wastewater treatment equipment. The early construction cost and the floor space are greatly saved, and the later operation is greatly saved, but the prior art is slightly insufficient considering that the generated fine particles are difficult to precipitate and easy to be polluted by a membrane, and the pH value of the treated water is lower.|DISCLOSURE|Disclosure of Invention|[0006] The technical problem to be solved is as follows:|aiming at the defects of the prior art, the method solves the problems that the existing cost is higher, and the existing method is not suitable for the wastewater containing solid particles with high salinity and complete dissolution; provides a ternary modified sludge carbon fluorine removal agent and a preparation method thereof.|[0007] The technical scheme is as follows:|in order to achieve the purpose, the application is realized by the following technical scheme:|a ternary modified sewage peat defluorinating agent and a preparation method thereof are disclosed, wherein the preparation method comprises the following specific steps:|the first step is as follows: pyrolyzing the dried sludge powder at 650-700 ℃ for 60-90min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2-2.5, then pyrolyzing the mixture for 60-90min at the temperature of 650-700 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar;|dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the sludge-based biochar prepared in the step 2;|and fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7-7.5, fully stirring for 12-14 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge carbon defluorinating agent.|[0008] As a preferred technical scheme of the invention: the aluminum chloride in the third step: cerium chloride: the molar ratio of the ferric chloride is 2:1: 0.01-0.05.|[0009] As a preferred technical scheme of the invention: and in the third step, the mass-volume ratio of the biochar to the ternary modifier is 1-2g:50 mL.|[0010] As a preferred technical scheme of the invention: before the sludge-based biochar is mixed with the ternary modifier in the third step, 100 parts of sludge-based biochar, 1-5 parts of lanthanum chloride hydrate, 3-7 parts of disodium hydrogen phosphate, 2-6 parts of chitosan, 3-5 parts of light magnesium oxide and 1-3 parts of ethylenediamine are weighed according to the mass part ratio, ultrasonically dispersed for 2 hours, centrifuged at 3000rpm, ground after vacuum drying, sieved by a 200-mesh and 400-mesh sieve to treat the sludge-based biochar, and then the ternary modifier is added according to the mass volume ratio of the treated sludge-based biochar to the ternary modifier of 1-2g:50 mL.|[0011] As a preferred technical scheme of the invention: the concentration of the sodium hydroxide solution in the fourth step is 1-3 mol/L.|[0012] As a preferred technical scheme of the invention: the temperature of the drying in the second step and the fourth step is 60-90 ℃.|[0013] The application also discloses the ternary modified sludge carbon defluorinating agent prepared by the preparation method.|[0014] Has the advantages that:|the application provides a ternary modified sludge carbon defluorinating agent and a preparation method thereof, and compared with the prior art, the ternary modified sludge carbon defluorinating agent has the following beneficial effects:|1. the method provides a new way for the destination of the sludge, so that the sludge becomes an economic and feasible material which is not influenced by seasons, and the method can be widely applied to the removal of fluoride in a water environment;|2. the prepared defluorination material has good adsorption performance, large adsorption capacity and rich and environment-friendly raw materials.|[0015] 3. Compared with the prior art, the invention further enlarges the pore volume and the pore diameter of the biochar through the potassium acetate, thereby better loading the metal composite component in the pore canal of the sludge-based biochar and finally synthesizing the biological defluorinating agent with high adsorption efficiency.|[0016] 4. The specific surface area of the biochar is enlarged by adopting a specific preparation process, oxygen-containing functional groups and metal oxides are introduced, and the components interact with each other, so that a better synergistic effect is exerted.|[0017] 5. The sludge-based biological adsorption material improves the performance of the composite rare earth high-polymer aluminum-based fluorine agent, and can widen the application range to alkalinity reaching 2-11.|[0018] 6. Under the action of oxygen-containing functional groups and metal ions on the surface of the biochar, the components have better synergistic interaction, the pH range of adsorption is widened, and the method can be better applied to removal of fluoride in wastewater.|[0019] 7. The removal rate of 20mg/L fluoride reaches more than 95%, the adsorption capacity is 80-100 mg/g, and the water environment adaptive pH range is 2-11.|[0020] 8. The cost is low; the adsorption capacity is greatly improved; the application range is greatly widened.|DRAWINGS DESCRIPTION|[0021] Description of the drawings:|FIG. 1 is a graph showing the absorbance of the present application at various pH values at an initial concentration of 20 mg/L.|[0022] FIG. 2 is a graph of absorbance of the present application at various initial concentrations at an initial pH of 6.|INVENTION MODE|Detailed Description|[0024] The following will further explain the embodiments and working procedures of the present invention by referring to examples.|[0025] Example 1:|a ternary modified sewage peat defluorinating agent and a preparation method thereof, the steps are as follows:|the first step is as follows: pyrolyzing the dried sludge powder at 700 ℃ for 90min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2.5, then pyrolyzing the mixture for 90min at 700 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar; the drying temperature is 90 ℃;|dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier; weighing 100 parts of sludge-based biochar, 1-5 parts of lanthanum chloride hydrate, 3-7 parts of disodium hydrogen phosphate, 2-6 parts of chitosan, 3-5 parts of light magnesium oxide and 1-3 parts of ethylenediamine according to the mass part ratio, performing ultrasonic dispersion for 2 hours, centrifuging at the speed of 3000rpm, drying in vacuum, grinding, treating the sludge-based biochar through a 200-mesh and 400-mesh sieve, and then adding a ternary modifier into the sludge-based biochar according to the mass volume ratio of the treated sludge-based biochar to the ternary modifier of 2g:50mL to fully mix the sludge-based biochar; the aluminum chloride in the third step: cerium chloride: the molar ratio of ferric chloride is 2:1: 0.05;|fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7.5, fully stirring for 14 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge coal defluorinating agent; the concentration of the sodium hydroxide solution in the fourth step is 3 mol/L; the temperature of drying was 90 ℃.|[0026] Example 2:|a ternary modified sewage peat defluorinating agent and a preparation method thereof, the steps are as follows:|the first step is as follows: pyrolyzing the dried sludge powder at 680 ℃ for 70min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2.2, then pyrolyzing the mixture for 70min at 680 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar; the drying temperature is 70 ℃;|thirdly, dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the biochar prepared in the step 2; the aluminum chloride in the third step: cerium chloride: the molar ratio of ferric chloride is 2:1: 0.03; in the third step, the mass-volume ratio of the biochar to the ternary modifier is.5 g:50 mL;|fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7.3, fully stirring for 13 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge coal defluorinating agent; the concentration of the sodium hydroxide solution in the fourth step is 2 mol/L; the temperature of drying was 70 ℃.|[0027] Example 3:|a ternary modified sewage peat defluorinating agent and a preparation method thereof, the steps are as follows:|the first step is as follows: pyrolyzing the dried sludge powder at 650 ℃ for 60min to obtain sludge biochar;|secondly, mixing the sludge biochar with potassium acetate according to the mass ratio of 1:2, then pyrolyzing the mixture for 60min at 650 ℃, centrifuging, washing, drying and crushing the mixture to obtain sludge-based biochar; the drying temperature is 60 ℃;|thirdly, dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the biochar prepared in the step 2; the aluminum chloride in the third step: cerium chloride: the molar ratio of ferric chloride is 2:1: 0.01; in the third step, the mass-volume ratio of the biochar to the ternary modifier is 1g:50 mL;|fourthly, dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7, fully stirring for 12 hours, centrifuging, washing, drying and crushing to obtain the ternary modified sludge coal defluorinating agent; the concentration of the sodium hydroxide solution in the fourth step is 1 mol/L; the temperature of drying was 60 ℃.|[0028] The parameters of pyrolysis temperature, activation temperature, alkali concentration, metal ion proportion, stirring time and the like are controlled within a set range, different products are obtained, and the adsorption capacity of the products is changed between 80 and 100 mg/g.|[0029] Finally, the above embodiments are only for illustrating the technical solutions of the present invention and not for limiting, and other modifications or equivalent substitutions made by the technical solutions of the present invention by the person skilled in the art shall be covered by the scope of the claims of the present invention without departing from the spirit and scope of the technical solutions of the present invention. Family Number|(97651204)|97651204|Abstract|(CN113786806 A)|The invention discloses a ternary modified sludge carbon fluorine removal agent and a preparation method thereof . The preparation method comprises the following steps : pyrolyzing dried sludge powder for 60-90 min at a temperature of 650-700 DEG C so as to obtain sludge biochar ; mixing the sludge biochar with potassium acetate according to a mass ratio of 1 : ( 2-2.5 ) , then conducting pyrolyzing at 650-700 DEG C for 60-90 minutes , and successively performing centrifuging , washing , drying and crushing to obtain sludge - based biochar ; dissolving aluminum chloride , cerium chloride and ferric chloride in deionized water to prepare a ternary modifier , and fully mixing the ternary modifier with the biochar prepared in the step 2 ; dropwise adding a sodium hydroxide solution into the mixed solution , adjusting the pH value of the solution to 7-7.5, conducting full stirring for 12-14 hours , and successively performing centrifuging , washing , drying and crushing to obtain the ternary modified sludge carbon fluorine removal agent . According to the ternary modified sludge carbon fluorine removal agent , the removal rate of fluoride with 20 mg / L reaches 95% or above , adsorption capacity is 80-100 mg / g , and a water environment adaptive pH range is 2-11. |CPC codes|(CN113786806 A)|B01J - 020/02/07 |B01J - 020/02/29 |B01J - 020/02/48 |B01J - 020/02/7 |B01J - 020/04/1 |B01J - 020/20 |B01J - 2220/4887 |IPC codes|(CN113786806 A)|B01J - 020/20 |B01J - 020/30 |Title|(CN113786806 A)|Ternary modified sludge carbon fluorine removal agent and preparation method thereof | Chemical engineering|Environmental technology B01J-020/02/07|B01J-020/02/29|B01J-020/02/48|B01J-020/02/7|B01J-020/04/1|B01J-020/20|B01J-2220/4887|C02F-001/28/1|C02F-001/28/3|C02F-2101/14 B01J-020/02/07|B01J-020/02/29|B01J-020/02/48|B01J-020/02/7|B01J-020/04/1|B01J-020/20|B01J-2220/4887|C02F-001/28/1|C02F-001/28/3|C02F-2101/14 B01J-020/20|B01J-020/30|C02F-001/28|C02F-101/14 B01J-020/20|B01J-020/30|C02F-001/28|C02F-101/14 CN120838367|CN120532457|CN120230074|CN118002089|CN117228812|CN117263350B CN120838367 116462205 WHO=Examiner SELF=N CAT=A|CN120532457 115778663 WHO=Examiner SELF=N CAT=A|CN120230074 115121815 WHO=Examiner SELF=N CAT=A|CN118002089 109732382 WHO=Examiner SELF=Y CAT=A|CN117228812 107757525 WHO=Examiner SELF=N CAT=A|CN117263350B 107889498 WHO=Examiner SELF=N CN110947362|CN110947361|CN110586031|WO2018110852 CN110947362 88119466 WHO=Examiner SELF=Y CAT=Y|CN110947361 88123697 WHO=Examiner SELF=Y CAT=A|CN110586031 87034858 WHO=Examiner SELF=N CAT=A|WO2018110852 79305564 WHO=Examiner SELF=N CAT=A JUNJIE ZHANG ET AL.: &quot;Sludge-based biochar activation to enhance Pb(II) adsorption&quot;, 《FUEL》 (Cat. Y) WO2018110852; CN110586031; CN110947361; CN110947362 REVOKED (CN113786806)|REVOKED DEAD (CN113786806)|DEAD (CN113786806)|LEGAL DETAILS FOR CN113786806|Actual or expected expiration date=2024-09-13|Legal state=DEAD|Status=REVOKED|Event publication date=2021-09-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202111162973|Application date=2021-09-30|Standardized application number=2021CN-1162973|Event publication date=2021-12-14|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN113786806|Publication stage code=A|Publication date=2021-12-14|Standardized publication number=CN113786806|Event publication date=2021-12-14|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2021-12-31|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-09-13|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSIdGTytcq+mlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000060431753&ekey=2228&xpn=CN113786806&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=vHVEmUGfF8i5tcZF7eiMeZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN113786806)|CN (CN113786806)|NAME=NANTONG UNIVERSITY , COUNTRY=CN (CN113786806)|NAME=QIAN CHAO;NANJING JINGWEI PATENT & TRADEMARK AGENCY CO., LTD , REG=32200 (CN113786806)|NAME=YE ZHANGQING|NAME=LI SHUSHU|NAME=SONG MINGSHAN|NAME=ZHOU QINGWEN 0 1 Titre: (CN113786806)|Ternary modified sludge carbon fluorine removal agent and preparation method thereof Résumé: (CN113786806)|The invention discloses a ternary modified sludge carbon fluorine removal agent and a preparation method thereof. The preparation method comprises the following steps: pyrolyzing dried sludge powder for 60-90 min at a temperature of 650-700 DEG C so as to obtain sludge biochar; mixing the sludge biochar with potassium acetate according to a mass ratio of 1: (2-2.5), then conducting pyrolyzing at 650-700 DEG C for 60-90 minutes, and successively performing centrifuging, washing, drying and crushing to obtain sludge-based biochar; dissolving aluminum chloride, cerium chloride and ferric chloride in deionized water to prepare a ternary modifier, and fully mixing the ternary modifier with the biochar prepared in the step 2; dropwise adding a sodium hydroxide solution into the mixed solution, adjusting the pH value of the solution to 7-7.5, conducting full stirring for 12-14 hours, and successively performing centrifuging, washing, drying and crushing to obtain the ternary modified sludge carbon fluorine removal agent. According to the ternary modified sludge carbon fluorine removal agent, the removal rate of fluoride with 20 mg/L reaches 95% or above, adsorption capacity is 80-100 mg/g, and a water environment adaptive pH range is 2-11. 43 Abstract gpt-4o-mini no The article focuses on a carbon fluorine removal agent and its preparation method, which does not relate to accelerated weathering or CO₂ capture.
47 CN202211535515 CN202211535515 CN115744901|CN115744901 103975415 CN115744901 B 2024-01-23 [CN115744901B]|CN115744901 A 2023-03-07 [CN115744901] 2022-12-02 2022-12-02 2024-01-23|2023-03-07 (CN115744901B)|2024-01-23 (CN115744901)|2042-12-02 (CN115744901)|Lanthanum modified magnetic sludge hydrothermal carbon, preparation method thereof and application thereof in removing phosphorus in water (CN115744901)|The invention discloses lanthanum-modified magnetic sludge hydrothermal carbon, a preparation method thereof and application of the lanthanum-modified magnetic sludge hydrothermal carbon in removal of phosphorus in water, and belongs to the technical field of sludge recycling and water treatment. The method for preparing the lanthanum-modified magnetic sludge hydrothermal carbon comprises the following steps: soaking and cleaning sludge in water to remove impurities, performing freezing pore-forming and vacuum drying, and crushing and sieving to obtain pretreated sludge; taking ascorbic acid as a reducing agent, adding the pretreated sludge, an iron source and a lanthanum source, uniformly mixing to obtain a mixed solution, adjusting the pH value of the mixed solution to 11-12, and carrying out hydrothermal carbonization reaction to obtain the lanthanum modified magnetic sludge hydrothermal carbon. The lanthanum modified magnetic sludge hydrothermal carbon is prepared through one-step hydrothermal carbonization, has good adsorption performance and can be used for removing phosphorus in water. ZHONGYUAN UNIVERSITY OF TECHNOLOGY (CN115744901)|ZHONGYUAN UNIVERSITY OF TECHNOLOGY ([CN])|(CN115744901)|ZHONGYUAN UNIVERSITY OF TECHNOLOGY ([CN]) GONG WEIJIN|HUANG LEI|GUO LINA|LIU YUE|ZHOU ZIZHEN|ZHAO FUWANG (CN115744901)|GONG WEIJIN|HUANG LEI|GUO LINA|LIU YUE|ZHOU ZIZHEN|ZHAO FUWANG|(CN115744901)|GONG WEIJIN|HUANG LEI|GUO LINA|LIU YUE|ZHOU ZIZHEN|ZHAO FUWANG (CN115744901)|LIANG JING;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 61223 (CN115744901)|The problems cause that the carbonization modification operation for preparing the biochar is complicated and complicated, the preparation cost is high, and the application is difficult to realize.| (CN115744901)|1. The preparation method of the lanthanum modified magnetic sludge hydrothermal carbon is characterized by comprising the following steps of:step 1, sludge pretreatmentImmersing municipal sludge in water, cleaning to remove impurities, freezing for pore-forming, vacuum drying, crushing and sieving to obtain pretreated sludge;step 2, lanthanum modified magnetic sludge hydro-thermal carbonAnd (3) taking ascorbic acid as a reducing agent, adding the pretreated sludge prepared in the step (1), an iron source and a lanthanum source, uniformly mixing to obtain a mixed solution, regulating the pH value of the mixed solution to 11-12, aging and stirring, and performing hydrothermal carbonization reaction to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|8. The application of the lanthanum-modified magnetic sludge hydrothermal carbon in removing phosphorus in water, which is characterized in that the lanthanum-modified magnetic sludge hydrothermal carbon is added into a phosphorus-containing aqueous solution as an adsorbent, and after the adsorption process reaches equilibrium, the lanthanum-modified magnetic sludge hydrothermal carbon is separated from a water body under the action of an externally applied magnetic field to obtain a phosphorus-removed solution and the lanthanum-modified magnetic sludge hydrothermal carbon reaching adsorption equilibrium.| (CN115744901)|Aiming at the problems, the invention provides lanthanum-modified magnetic sludge hydrothermal carbon, a preparation method and application thereof in removing phosphorus in water, wherein metal modification, magnetization and activation of biochar are all carried out in a carbonization step, complex preparation conditions are not needed, and the lanthanum-modified magnetic sludge hydrothermal carbon with good adsorption performance can be prepared by one-step hydrothermal carbonization. The first object of the invention is to provide a preparation method of lanthanum modified magnetic sludge hydrothermal carbon, which comprises the following steps:|The invention discloses lanthanum modified magnetic sludge hydrothermal carbon, a preparation method and application thereof in removing phosphorus in water, and belongs to the technical field of sludge recycling and water treatment.|The invention relates to the technical field of sludge recycling and water treatment, in particular to lanthanum modified magnetic sludge hydrothermal carbon, a preparation method and application in removing phosphorus in water.| |(CN115744901)|SLUDGE HYDROTHERMAL CARBON(100,63)|LANTHANUM(100,34)|MAGNETIC SLUDGE HYDROTHERMAL CARBON(100,34)|PHOSPHORUS(100,18)|PRETREATMENT SOAKING SLUDGE(55,1)|PRETREATED SLUDGE(49,7)|SLUDGE HYDROTHERMAL CHARCOAL(46,2)|SLUDGE RECYCLING(43,2)|HYDROTHERMAL CARBONIZATION(21,3)|PRETREATED SLUDGE POWDER(20,8)|LANTHANUM DOSAGE(20,1)|LANTHANUM SOURCE(19,8)|FREEZING(17,7)|PHOSPHORUS REMOVAL(16,8)|MIXED SOLUTION(16,7)|MUNICIPAL SLUDGE(16,3)|IMPURITY(15,3)|INTERCEPTED MATTER(15,1)|IRON SOURCE(14,10)|IRON ION(13,4)|CRUSHING(12,8)|ADSORPTION BALANCE(12,3)|CARBONIZATION TREATMENT(12,2)|LANTHANUM ION(12,2)|MIXED LIQUOR(12,1)|SLUDGE(11,15)|MOLAR RATIO(11,4)|ADSORPTION PERFORMANCE(11,3)|PREPARATION COST(11,1)|STEP HYDROTHERMAL CARBONIZATION(11,1)|DEWATERED SLUDGE(10,7)|HYDROTHERMAL KETTLE(10,7)|ADSORPTION REACTION(10,2)|ASCORBIC ACID(9,14)|BIOCHAR(9,12)|SLUDGE PRETREATMENT(9,6)|AGING(9,2)|CARBONIZATION MODIFICATION OPERATION(9,1)|AQUEOUS SOLUTION(8,4)|ADSORBENT(8,2)|WATER PHOSPHORUS REMOVAL(8,1)|LANTHANUM NITRATE(7,5)|WATER TREATMENT(7,2)|SUBSTANCE INTERCEPTION(6,4)|REDUCING AGENT(6,3)|PORE(6,2)|VACUUM DRYING(6,2)|BIOMASS CARBONIZATION FURNACE(6,1)|SIEVE MESH(6,1)|SLUDGE POLLUTION DUAL ATTRIBUTE(6,1)|LANTHANUM CHLORIDE(5,8)|WATER BATH SHAKER(5,8)|FREEZE DRIED SLUDGE(5,6)|FERRIC SULFATE(5,4)|CARRYING OUT HYDROTHERMAL CARBONIZATION(5,2)|SEWAGE SLUDGE RESOURCE RECYCLING(5,1)|SLUDGE HARMLESS RECYCLING(5,1)|SLUDGE RESOURCE UTILIZATION(5,1)|REACTION TEMPERATURE(4,8)|PHOSPHATE SOLUTION(4,6)|FREEZE DRYING PRETREATMENT(4,2)|TRAPPED SUBSTANCE(4,2)|BIOCHAR MAGNETIZATION(4,1)|BIOCHEMICAL REAGENT(4,1)|BIOMASS RESOURCE UTILIZATION(4,1)|DRYING INTERCEPTED SUBSTANCE(4,1)|FERRIC NITRATE NONAHYDRATE(4,1)|FERRIC TRICHLORIDE HEXAHYDRATE(4,1)|HENAN PROVINCE(4,1)|MAGNETIC SLUDGE BIOCHAR(4,1)|MOLYBDENUM ANTIMONY ANTISPECTROPHOTOMETRY(4,1)|NORFLOXACIN SLUDGE(4,1)|SLUDGE DEHYDRATION(4,1)|PURE WATER(3,19)|FREEZE DRYER(3,5)|PREFREEZING(3,5)|MAGNETIC FERRIC OXIDE(3,3)|IRON SOURCE MASS RATIO(3,2)|SLUDGE PYROLYTIC CARBON(3,2)|SOAKING TIME(3,2)|CREATIVE EFFORT(3,1)|FIXING POLLUTANT(3,1)|ICE SUBLIMATION(3,1)|POROUS BIOCHAR(3,1)|RECYCLING RESOURCE(3,1)|REPORTED DOMESTIC(3,1)|SLUDGE CONTAMINATION(3,1)|TETRACYCLIC SCIENCE(3,1)|XINZHENG CITY(3,1)|FILTERED WATER(2,8)|BEAKER(2,6)|HYDROTHERMAL REACTION CONDITION(2,6)|POTASSIUM HYDROXIDE SOLUTION(2,6)|FERRIC CHLORIDE(2,5)|AGED(2,4)|BASIC INVENTIVE CONCEPT(2,1)|BLAST OVEN(2,1)|DRY PYROLYSIS(2,1)|GROUND SLUDGE(2,1)|HYDROTHERMAL CARBON PHOSPHORUS(2,1)|HYDROTHERMAL CARBONIZATION REACTION(2,1)|HYDROTHERMAL CONDITION(2,1)|HYDROTHERMAL TREATMENT(2,1)|MULTIMETAL(2,1)|RESOURCE DOUBLE BENEFIT(2,1)|RICH OXYGEN(2,1)|ROTATION SPEED(2,1)|SLUDGE MODIFICATION(2,1)|SLUDGE YIELD(2,1)|SOLVOTHERMAL(2,1)|TERMINATION CLEAR SOLUTION PHOSPHORUS(2,1)|WATER BODY(2,1)| (CN115744901)|1. The preparation method of the lanthanum modified magnetic sludge hydrothermal carbon is characterized by comprising the following steps of:|step 1, sludge pretreatment|Immersing municipal sludge in water, cleaning to remove impurities, freezing for pore-forming, vacuum drying, crushing and sieving to obtain pretreated sludge;|step 2, lanthanum modified magnetic sludge hydro-thermal carbon|And (3) taking ascorbic acid as a reducing agent, adding the pretreated sludge prepared in the step (1), an iron source and a lanthanum source, uniformly mixing to obtain a mixed solution, regulating the pH value of the mixed solution to 11-12, aging and stirring, and performing hydrothermal carbonization reaction to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|2. The method for preparing the lanthanum-modified magnetic sludge hydrothermal carbon according to claim 1, wherein in the step 1, the soaking time is 1-3h, the freezing pore-forming method is pre-freezing and vacuumizing for 1-2d, and the sieving mesh number is 60-80 mesh.|3. The method for preparing lanthanum-modified magnetic sludge hydrothermal carbon according to claim 1, wherein in the step 2, the mass ratio of the iron source to the pretreated sludge powder is 2:1; the mole ratio of lanthanum ions in the lanthanum source to iron ions in the iron source is 2-2.5:1; the molar ratio of the ascorbic acid to the iron ions is 0.05-0.1:1.|4. The method for preparing lanthanum-modified magnetic sludge hydrothermal carbon according to claim 1, wherein in the step 2, the iron source is ferric trichloride, ferric sulfate or ferric nitrate, and the lanthanum source is lanthanum nitrate or lanthanum chloride.|5. The method for preparing lanthanum-modified magnetic sludge hydrothermal carbon according to claim 1, wherein in the step 2, the reaction temperature of the carbonization reaction is 200-210 ℃ and the reaction time is 10-11h;|and after carbonization treatment, washing and suction-filtering the obtained product by using pure water and ethanol in turn until the filtered water is clear, and drying the retentate to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|6. The method for preparing lanthanum-modified magnetic sludge hydrothermal carbon according to claim 1, wherein the pH of the mixed solution is adjusted by potassium hydroxide.|7. A lanthanum-modified magnetic sludge hydrothermal char prepared by the method of any one of claims 1-6.|8. The application of the lanthanum-modified magnetic sludge hydrothermal carbon in removing phosphorus in water, which is characterized in that the lanthanum-modified magnetic sludge hydrothermal carbon is added into a phosphorus-containing aqueous solution as an adsorbent, and after the adsorption process reaches equilibrium, the lanthanum-modified magnetic sludge hydrothermal carbon is separated from a water body under the action of an externally applied magnetic field to obtain a phosphorus-removed solution and the lanthanum-modified magnetic sludge hydrothermal carbon reaching adsorption equilibrium.|9. The use of lanthanum modified magnetic sludge hydro-thermal char of claim 8 for phosphorous removal in water, wherein the total phosphorous concentration in the phosphorous-containing aqueous solution is 100-200mg/L, pH is 7.0±0.2; the adding amount of lanthanum modified magnetic sludge hydrothermal carbon is 1.78-3.6g/L;|10. the use of lanthanum-modified magnetic sludge hydrothermal carbon in removing phosphorus from water according to claim 8, wherein the temperature of the adsorption reaction is 25±0.5 ℃, and the rotation speed of the water bath shaker is 120-150rpm. (CN115744901)|TECHNICAL FIELD|[0001] The invention relates to the technical field of sludge recycling and water treatment, in particular to lanthanum modified magnetic sludge hydrothermal carbon, a preparation method and application in removing phosphorus in water.|BACKGROUND ART|[0002] As the sewage treatment rate increases year by year, the sludge is used as a by-product of sewage treatment, and the sludge yield is correspondingly increased, so that the sludge treatment problem needs to be effectively solved. At present, the common sludge treatment technology not only can generate a large amount of secondary pollutants such as percolate, dioxin and the like in the treatment process, but also does not realize the recycling of sludge. From the viewpoints of reducing carbon emission and recycling resources, the dual properties of sludge pollution and resources must be considered to promote recycling of sewage sludge resources and energy sources.|[0003] Biomass carbonization technology is an emerging technology for biomass resource utilization. The biomass charcoal is mainly carbonized and fixed in a form of steady-state charcoal, so that a novel biomass charcoal product is formed. Several researches show that the sludge is rich in carbon and other active elements, and is a promising raw material for manufacturing biochar. Research shows that the hydrothermal carbon has more abundant oxygen-containing functional groups than the pyrolytic carbon, which means that the hydrothermal carbon retains more active sites than the biochar obtained by dry pyrolysis, suggesting that the hydrothermal carbon may be more advantageous in promoting adsorption and fixing of pollutants. At present, a large number of researches and reports on sludge pyrolytic carbon are available, and most of the sludge pyrolytic carbon is used for adsorbing heavy metals or preparing a catalyst to degrade pollutants. And less research is conducted on the adsorption and recovery of sludge hydro-thermal carbon phosphorus. Chinese patent No. CN202210404079.9 discloses a method for preparing biochar from water by removing tetracycline magnetic sludge, chinese patent No. CN202111485720.8 discloses a method for preparing biochar from water by removing norfloxacin sludge, however, studies for preparing hydrothermal carbon from water by modifying lanthanum and iron have been freshly reported.|[0004] In the research at home and abroad reported at present, the charcoal is magnetized by coprecipitation (requiring nitrogen atmosphere) and solvothermal method (using chemicals such as ethylene glycol, polyethylene glycol, sodium acetate, urea and the like); in addition, the preparation of the multi-metal modified biochar requires the carbonization and modification steps to be separated or the continuous carbonization and modification to be carried out for many times, and then the biochar is activated independently to improve the adsorption performance. The problems cause that the carbonization modification operation for preparing the biochar is complicated and complicated, the preparation cost is high, and the application is difficult to realize.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the problems, the invention provides lanthanum-modified magnetic sludge hydrothermal carbon, a preparation method and application thereof in removing phosphorus in water, wherein metal modification, magnetization and activation of biochar are all carried out in a carbonization step, complex preparation conditions are not needed, and the lanthanum-modified magnetic sludge hydrothermal carbon with good adsorption performance can be prepared by one-step hydrothermal carbonization.|[0006] The first object of the invention is to provide a preparation method of lanthanum modified magnetic sludge hydrothermal carbon, which comprises the following steps:|[0007] step 1, sludge pretreatment|[0008] Soaking and cleaning the sludge in water to remove impurities, freezing and pore-forming, vacuum drying, and crushing and sieving to obtain pretreated sludge;|[0009] step 2, lanthanum modified magnetic sludge hydro-thermal carbon|[0010] And (3) taking ascorbic acid as a reducing agent, adding the pretreated sludge prepared in the step (1), an iron source and a lanthanum source, uniformly mixing to obtain a mixed solution, adjusting the pH value of the mixed solution to 11-12, and performing hydrothermal carbonization reaction to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0011] Preferably, in the step 1, the sludge is municipal sludge, the soaking time is 1-3h, the freezing pore-forming method is prefreezing and vacuumizing for 1-2d, and the sieving mesh number is 60-80 mesh.|[0012] Preferably, in the step 2, the mass ratio of the iron source to the pretreated sludge powder is 2:1; the mole ratio of lanthanum ions in the lanthanum source to iron ions in the iron source is 2-2.5:1; the molar ratio of the ascorbic acid to the iron ions is 0.05-0.1:1.|[0013] Preferably, in the step 2, the iron source is ferric trichloride, ferric sulfate or ferric nitrate, and the lanthanum source is lanthanum nitrate or lanthanum chloride.|[0014] Preferably, in the step 2, the reaction temperature of the carbonization reaction is 200-210 ℃ and the reaction time is 10-11h; and after carbonization treatment, washing and suction-filtering the obtained product by using pure water and ethanol in turn until the filtered water is clear, and drying the retentate to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0015] Preferably, potassium hydroxide is used to adjust the pH of the mixture.|[0016] The second purpose of the invention is to provide the lanthanum modified magnetic sludge hydrothermal carbon prepared by the preparation method.|[0017] The third object of the invention is to provide the application of the lanthanum-modified magnetic sludge hydrothermal carbon in removing phosphorus in water, wherein the lanthanum-modified magnetic sludge hydrothermal carbon is added into a phosphorus-containing aqueous solution as an adsorbent, and after the adsorption process reaches equilibrium, the lanthanum-modified magnetic sludge hydrothermal carbon is separated from a water body under the action of an externally applied magnetic field, so that a phosphorus-removed solution and the lanthanum-modified magnetic sludge hydrothermal carbon reaching adsorption equilibrium are obtained.|[0018] Preferably, the concentration of total phosphorus in the phosphorus-containing aqueous solution is 100-200mg/L, pH and is 7.0+/-0.2; the adding amount of lanthanum modified magnetic sludge hydrothermal carbon is 1.78-3.6g/L;|[0019] preferably, the temperature of the adsorption reaction is 25+/-0.5 ℃ and the rotating speed of the water bath shaking table is 120-150rpm.|[0020] Compared with the prior art, the invention has the following beneficial effects:|[0021] the invention provides a technical scheme for harmless recycling of sludge, namely carbonization and modification of the sludge are completed through hydrothermal reaction at a lower temperature of 200-210 ℃, and the reaction mechanism is as follows: the biomass in the freeze-dried sludge is subjected to decarboxylation, polymerization and aromatization to form porous biochar, lanthanum chloride is converted into lanthanum hydroxide for adhesion to finish metal loading, ferric chloride is reduced into magnetic ferric oxide by ascorbic acid to endow the magnetic ferric oxide with magnetism, and potassium hydroxide assists in pore forming, and finally the material preparation is finished. The prepared lanthanum modified magnetic sludge hydro-thermal carbon has larger adsorption capacity, low cost and double benefits of resources and environment.|DRAWINGS DESCRIPTION|[0022] Fig. 1 is a schematic flow chart of the preparation of lanthanum-modified magnetic sludge hydrothermal carbon.|INVENTION MODE|Detailed Description|[0023] The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0024] The experimental methods in the following examples and comparative examples are conventional methods unless otherwise specified. The test materials used in the following examples or comparative examples were purchased from conventional biochemical reagent stores unless otherwise specified. The freeze drying in the examples is carried out in an LGJ-10C freeze dryer of Beijing four-ring scientific instrument factory, the hydrothermal carbonization is carried out in a high-temperature high-pressure hydrothermal kettle, and the heating is carried out by using a blast oven. The municipal sludge in the examples was obtained from a domestic sewage treatment plant in new zheng city, zheng state, henan province. The ferric trichloride used in the invention is ferric trichloride hexahydrate, ferric nitrate is ferric nitrate nonahydrate, ferric sulfate is anhydrous ferric sulfate, lanthanum nitrate is anhydrous lanthanum nitrate, and lanthanum chloride is anhydrous lanthanum chloride.|[0025] According to the invention, the dehydrated sludge is fully cleaned in water to remove large-particle impurities, is frozen for pore forming after being fully soaked in water, and is subjected to freeze drying pretreatment to obtain sludge powder with larger porosity and specific surface area, so that the surface physical properties of the sludge hydrothermal carbon are improved. And then vacuumizing to completely sublimate the ice to finish drying, and finally crushing and sieving to obtain pretreated sludge powder.|[0026] Then uniformly mixing the pretreated sludge powder with an iron source, a lanthanum source and ascorbic acid, adding potassium hydroxide, transferring into a hydrothermal kettle for hydrothermal treatment, wherein the potassium hydroxide is used for regulating pH to be alkaline so as to generate precipitated load metal, and also plays a role in pore forming in the hydrothermal reaction so as to form biochar with a larger pore structure; adding ascorbic acid to reduce ferric iron in ferric trichloride under hydrothermal condition to generate magnetic ferric oxide, and finishing magnetization. And preparing the lanthanum modified magnetic sludge hydrothermal carbon.|[0027] Example 1|[0028] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0029] step 1, sludge pretreatment|[0030] Fully soaking the dehydrated sludge in pure water for 2 hours, then pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, and then crushing and grinding the dehydrated sludge, and sieving the crushed and ground dehydrated sludge with a 60-mesh sieve for storage.|[0031] And 2, preparing a solution.|[0032] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0033] Step 3, sludge hydrothermal carbon preparation|[0034] 0.5g of pretreated sludge powder, 1g of ferric chloride, 1.8147g of lanthanum chloride and 0.0326g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, added with potassium hydroxide to adjust the pH to 11-12, aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 200 ℃ and the reaction time is 10 hours. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0035] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0036] 0.05g of biochar was placed in a 100mL beaker containing 20mL of 100 (or 200) mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and then the mixture was shaken in a water bath at 25.+ -. 0.5 ℃ for 12h at 120 rpm.|[0037] Example 2|[0038] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0039] step 1, sludge pretreatment|[0040] Fully soaking the dehydrated sludge in pure water for 1h, then pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, and then crushing and grinding the dehydrated sludge, and sieving the crushed and ground dehydrated sludge with a 80-mesh sieve for storage.|[0041] And 2, preparing a solution.|[0042] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0043] Step 3, sludge hydrothermal carbon preparation|[0044] 0.5g of pretreated sludge powder, 1g of ferric chloride, 2.2687g of lanthanum chloride and 0.0652g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, potassium hydroxide is added to adjust the pH to 11-12, and the mixture is aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 210 ℃ and the reaction time is 10 hours. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0045] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0046] 0.0356g of charcoal was placed in a 100mL beaker containing 20mL of 150mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and then the mixture was shaken in a water bath shaker at 25.+ -. 0.5 ℃ for 12 hours at 150rpm.|[0047] Example 3|[0048] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0049] step 1, sludge pretreatment|[0050] Fully soaking the dehydrated sludge in pure water for 1h, then pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, and then crushing and grinding the dehydrated sludge, and sieving the crushed and ground dehydrated sludge with a 70-mesh sieve for storage.|[0051] And 2, preparing a solution.|[0052] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0053] Step 3, sludge hydrothermal carbon preparation|[0054] 0.5g of pretreated sludge powder, 1g of ferric chloride, 2.0872g of lanthanum nitrate and 0.0456g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, potassium hydroxide is added to adjust the pH to 11-12, and the mixture is aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 205 ℃ and the reaction time is 10 hours. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0055] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0056] 0.072g of biochar was placed in a 100mL beaker containing 20mL of 100mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and the mixture was then shaken in a 25.+ -. 0.5 ℃ water bath shaker at 130rpm for 12h.|[0057] Example 4|[0058] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0059] step 1, sludge pretreatment|[0060] Fully soaking the dehydrated sludge in pure water for 1h, then pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, and then crushing and grinding the dehydrated sludge, and sieving the crushed and ground dehydrated sludge with a 80-mesh sieve for storage.|[0061] And 2, preparing a solution.|[0062] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0063] Step 3, sludge hydrothermal carbon preparation|[0064] 0.5g of pretreated sludge powder, 1g of ferric nitrate, 1.625g of lanthanum nitrate and 0.0218g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, added with potassium hydroxide to adjust the pH to 11-12, aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 200 ℃ and the reaction time is 11h. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0065] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0066] 0.05g of biochar was placed in a 100mL beaker containing 20mL of 200mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M NaOH, and then the mixture was shaken in a water bath shaker at 25.+ -. 0.5 ℃ for 12 hours at 120 rpm.|[0067] Example 5|[0068] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0069] step 1, sludge pretreatment|[0070] Soaking dehydrated sludge in pure water for 2 hours, pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, crushing and grinding the dehydrated sludge, and sieving with a 80-mesh sieve for storage.|[0071] And 2, preparing a solution.|[0072] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0073] Step 3, sludge hydrothermal carbon preparation|[0074] 0.5g of pretreated sludge powder, 1g of ferric sulfate, 2.4526g of lanthanum chloride and 0.04g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, added with potassium hydroxide to adjust the pH to 11-12, aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 200 ℃ and the reaction time is 10.5h. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0075] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0076] 0.05g of biochar was placed in a 100mL beaker containing 20mL of 100 (or 200) mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and then the mixture was shaken in a water bath at 25.+ -. 0.5 ℃ for 12h at 120 rpm.|[0077] Comparative example 1|[0078] In comparison with example 1, the procedure was as in example 1 except that the sludge used in this comparative example was dehydrated sludge (the water content of dehydrated sludge was 74.8%). The preparation method comprises the following specific steps:|[0079] and 1, preparing a solution.|[0080] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0081] Step 2, sludge hydrothermal carbon preparation|[0082] 1.9841g of dehydrated sludge, 1g of ferric chloride, 1.8147g of lanthanum chloride and 0.0326g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, potassium hydroxide is added to adjust the pH to 11-12, and stirring is carried out for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 200 ℃ and the reaction time is 10 hours. Washing and suction-filtering the obtained product with pure water and ethanol in turn for more than 3 times after the reaction is completed until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon|[0083] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the comparative example is applied to removing phosphorus in water, and comprises the following steps:|[0084] 0.05g of biochar was placed in a 100mL beaker containing 20mL of 100 (or 200) mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and then the mixture was shaken in a water bath at 25.+ -. 0.5 ℃ for 12h at 120 rpm.|[0085] To further verify the effectiveness of the lanthanum-modified magnetic sludge hydrothermal charcoal prepared in the present invention, using example 1 and comparative example 1 as examples, 0.45 μm syringe filter was used to filter after adsorption was completed, and 0.5mL of solution was used to determine the phosphorus concentration of the terminated supernatant by molybdenum-antimony spectrophotometry. The experiments were performed in three parallel groups and the specific data are shown in table 1.|[0086] TABLE 1 total phosphorus concentration of initial solution and adsorption stop serum|[0087] |[0088] From the table, the freeze-drying pretreatment can obviously improve the adsorption performance of the sludge hydrothermal carbon, and the maximum adsorption quantity of the sludge hydrothermal carbon is 56.08mg/g. The preparation process of the invention not only can effectively recycle the sludge, but also can effectively remove the phosphorus in the water, thereby realizing the common treatment of sewage and sludge. Meanwhile, the lanthanum modified magnetic sludge hydrothermal carbon achieving adsorption balance can be used as a slow-release phosphate fertilizer.|[0089] While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the following claims be interpreted as including the preferred embodiments and all such alterations and modifications as fall within the scope of the invention.|[0090] It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof. (CN115744901)|TECHNICAL FIELD|[0001] The invention relates to the technical field of sludge recycling and water treatment, in particular to lanthanum modified magnetic sludge hydrothermal carbon, a preparation method and application in removing phosphorus in water.|BACKGROUND ART|[0002] As the sewage treatment rate increases year by year, the sludge is used as a by-product of sewage treatment, and the sludge yield is correspondingly increased, so that the sludge treatment problem needs to be effectively solved. At present, the common sludge treatment technology not only can generate a large amount of secondary pollutants such as percolate, dioxin and the like in the treatment process, but also does not realize the recycling of sludge. From the viewpoints of reducing carbon emission and recycling resources, the dual properties of sludge pollution and resources must be considered to promote recycling of sewage sludge resources and energy sources.|[0003] Biomass carbonization technology is an emerging technology for biomass resource utilization. The biomass charcoal is mainly carbonized and fixed in a form of steady-state charcoal, so that a novel biomass charcoal product is formed. Several researches show that the sludge is rich in carbon and other active elements, and is a promising raw material for manufacturing biochar. Research shows that the hydrothermal carbon has more abundant oxygen-containing functional groups than the pyrolytic carbon, which means that the hydrothermal carbon retains more active sites than the biochar obtained by dry pyrolysis, suggesting that the hydrothermal carbon may be more advantageous in promoting adsorption and fixing of pollutants. At present, a large number of researches and reports on sludge pyrolytic carbon are available, and most of the sludge pyrolytic carbon is used for adsorbing heavy metals or preparing a catalyst to degrade pollutants. And less research is conducted on the adsorption and recovery of sludge hydro-thermal carbon phosphorus. Chinese patent No. CN202210404079.9 discloses a method for preparing biochar from water by removing tetracycline magnetic sludge, chinese patent No. CN202111485720.8 discloses a method for preparing biochar from water by removing norfloxacin sludge, however, studies for preparing hydrothermal carbon from water by modifying lanthanum and iron have been freshly reported.|[0004] In the research at home and abroad reported at present, the charcoal is magnetized by coprecipitation (requiring nitrogen atmosphere) and solvothermal method (using chemicals such as ethylene glycol, polyethylene glycol, sodium acetate, urea and the like); in addition, the preparation of the multi-metal modified biochar requires the carbonization and modification steps to be separated or the continuous carbonization and modification to be carried out for many times, and then the biochar is activated independently to improve the adsorption performance. The problems cause that the carbonization modification operation for preparing the biochar is complicated and complicated, the preparation cost is high, and the application is difficult to realize.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the problems, the invention provides lanthanum-modified magnetic sludge hydrothermal carbon, a preparation method and application thereof in removing phosphorus in water, wherein metal modification, magnetization and activation of biochar are all carried out in a carbonization step, complex preparation conditions are not needed, and the lanthanum-modified magnetic sludge hydrothermal carbon with good adsorption performance can be prepared by one-step hydrothermal carbonization.|[0006] The first object of the invention is to provide a preparation method of lanthanum modified magnetic sludge hydrothermal carbon, which comprises the following steps:|[0007] step 1, sludge pretreatment|[0008] Soaking and cleaning the sludge in water to remove impurities, freezing and pore-forming, vacuum drying, and crushing and sieving to obtain pretreated sludge;|[0009] step 2, lanthanum modified magnetic sludge hydro-thermal carbon|[0010] And (3) taking ascorbic acid as a reducing agent, adding the pretreated sludge prepared in the step (1), an iron source and a lanthanum source, uniformly mixing to obtain a mixed solution, adjusting the pH value of the mixed solution to 11-12, and performing hydrothermal carbonization reaction to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0011] Preferably, in the step 1, the sludge is municipal sludge, the soaking time is 1-3h, the freezing pore-forming method is prefreezing and vacuumizing for 1-2d, and the sieving mesh number is 60-80 mesh.|[0012] Preferably, in the step 2, the mass ratio of the iron source to the pretreated sludge powder is 2:1; the mole ratio of lanthanum ions in the lanthanum source to iron ions in the iron source is 2-2.5:1; the molar ratio of the ascorbic acid to the iron ions is 0.05-0.1:1.|[0013] Preferably, in the step 2, the iron source is ferric trichloride, ferric sulfate or ferric nitrate, and the lanthanum source is lanthanum nitrate or lanthanum chloride.|[0014] Preferably, in the step 2, the reaction temperature of the carbonization reaction is 200-210 ℃ and the reaction time is 10-11h; and after carbonization treatment, washing and suction-filtering the obtained product by using pure water and ethanol in turn until the filtered water is clear, and drying the retentate to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0015] Preferably, potassium hydroxide is used to adjust the pH of the mixture.|[0016] The second purpose of the invention is to provide the lanthanum modified magnetic sludge hydrothermal carbon prepared by the preparation method.|[0017] The third object of the invention is to provide the application of the lanthanum-modified magnetic sludge hydrothermal carbon in removing phosphorus in water, wherein the lanthanum-modified magnetic sludge hydrothermal carbon is added into a phosphorus-containing aqueous solution as an adsorbent, and after the adsorption process reaches equilibrium, the lanthanum-modified magnetic sludge hydrothermal carbon is separated from a water body under the action of an externally applied magnetic field, so that a phosphorus-removed solution and the lanthanum-modified magnetic sludge hydrothermal carbon reaching adsorption equilibrium are obtained.|[0018] Preferably, the concentration of total phosphorus in the phosphorus-containing aqueous solution is 100-200mg/L, pH and is 7.0+/-0.2; the adding amount of lanthanum modified magnetic sludge hydrothermal carbon is 1.78-3.6g/L;|[0019] preferably, the temperature of the adsorption reaction is 25+/-0.5 ℃ and the rotating speed of the water bath shaking table is 120-150rpm.|[0020] Compared with the prior art, the invention has the following beneficial effects:|[0021] the invention provides a technical scheme for harmless recycling of sludge, namely carbonization and modification of the sludge are completed through hydrothermal reaction at a lower temperature of 200-210 ℃, and the reaction mechanism is as follows: the biomass in the freeze-dried sludge is subjected to decarboxylation, polymerization and aromatization to form porous biochar, lanthanum chloride is converted into lanthanum hydroxide for adhesion to finish metal loading, ferric chloride is reduced into magnetic ferric oxide by ascorbic acid to endow the magnetic ferric oxide with magnetism, and potassium hydroxide assists in pore forming, and finally the material preparation is finished. The prepared lanthanum modified magnetic sludge hydro-thermal carbon has larger adsorption capacity, low cost and double benefits of resources and environment.|DRAWINGS DESCRIPTION|[0022] Fig. 1 is a schematic flow chart of the preparation of lanthanum-modified magnetic sludge hydrothermal carbon.|INVENTION MODE|Detailed Description|[0023] The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0024] The experimental methods in the following examples and comparative examples are conventional methods unless otherwise specified. The test materials used in the following examples or comparative examples were purchased from conventional biochemical reagent stores unless otherwise specified. The freeze drying in the examples is carried out in an LGJ-10C freeze dryer of Beijing four-ring scientific instrument factory, the hydrothermal carbonization is carried out in a high-temperature high-pressure hydrothermal kettle, and the heating is carried out by using a blast oven. The municipal sludge in the examples was obtained from a domestic sewage treatment plant in new zheng city, zheng state, henan province. The ferric trichloride used in the invention is ferric trichloride hexahydrate, ferric nitrate is ferric nitrate nonahydrate, ferric sulfate is anhydrous ferric sulfate, lanthanum nitrate is anhydrous lanthanum nitrate, and lanthanum chloride is anhydrous lanthanum chloride.|[0025] According to the invention, the dehydrated sludge is fully cleaned in water to remove large-particle impurities, is frozen for pore forming after being fully soaked in water, and is subjected to freeze drying pretreatment to obtain sludge powder with larger porosity and specific surface area, so that the surface physical properties of the sludge hydrothermal carbon are improved. And then vacuumizing to completely sublimate the ice to finish drying, and finally crushing and sieving to obtain pretreated sludge powder.|[0026] Then uniformly mixing the pretreated sludge powder with an iron source, a lanthanum source and ascorbic acid, adding potassium hydroxide, transferring into a hydrothermal kettle for hydrothermal treatment, wherein the potassium hydroxide is used for regulating pH to be alkaline so as to generate precipitated load metal, and also plays a role in pore forming in the hydrothermal reaction so as to form biochar with a larger pore structure; adding ascorbic acid to reduce ferric iron in ferric trichloride under hydrothermal condition to generate magnetic ferric oxide, and finishing magnetization. And preparing the lanthanum modified magnetic sludge hydrothermal carbon.|[0027] Example 1|[0028] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0029] step 1, sludge pretreatment|[0030] Fully soaking the dehydrated sludge in pure water for 2 hours, then pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, and then crushing and grinding the dehydrated sludge, and sieving the crushed and ground dehydrated sludge with a 60-mesh sieve for storage.|[0031] And 2, preparing a solution.|[0032] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0033] Step 3, sludge hydrothermal carbon preparation|[0034] 0.5g of pretreated sludge powder, 1g of ferric chloride, 1.8147g of lanthanum chloride and 0.0326g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, added with potassium hydroxide to adjust the pH to 11-12, aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 200 ℃ and the reaction time is 10 hours. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0035] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0036] 0.05g of biochar was placed in a 100mL beaker containing 20mL of 100 (or 200) mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and then the mixture was shaken in a water bath at 25.+ -. 0.5 ℃ for 12h at 120 rpm.|[0037] Example 2|[0038] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0039] step 1, sludge pretreatment|[0040] Fully soaking the dehydrated sludge in pure water for 1h, then pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, and then crushing and grinding the dehydrated sludge, and sieving the crushed and ground dehydrated sludge with a 80-mesh sieve for storage.|[0041] And 2, preparing a solution.|[0042] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0043] Step 3, sludge hydrothermal carbon preparation|[0044] 0.5g of pretreated sludge powder, 1g of ferric chloride, 2.2687g of lanthanum chloride and 0.0652g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, potassium hydroxide is added to adjust the pH to 11-12, and the mixture is aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 210 ℃ and the reaction time is 10 hours. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0045] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0046] 0.0356g of charcoal was placed in a 100mL beaker containing 20mL of 150mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and then the mixture was shaken in a water bath shaker at 25.+ -. 0.5 ℃ for 12 hours at 150rpm.|[0047] Example 3|[0048] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0049] step 1, sludge pretreatment|[0050] Fully soaking the dehydrated sludge in pure water for 1h, then pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, and then crushing and grinding the dehydrated sludge, and sieving the crushed and ground dehydrated sludge with a 70-mesh sieve for storage.|[0051] And 2, preparing a solution.|[0052] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0053] Step 3, sludge hydrothermal carbon preparation|[0054] 0.5g of pretreated sludge powder, 1g of ferric chloride, 2.0872g of lanthanum nitrate and 0.0456g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, potassium hydroxide is added to adjust the pH to 11-12, and the mixture is aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 205 ℃ and the reaction time is 10 hours. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0055] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0056] 0.072g of biochar was placed in a 100mL beaker containing 20mL of 100mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and the mixture was then shaken in a 25.+ -. 0.5 ℃ water bath shaker at 130rpm for 12h.|[0057] Example 4|[0058] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0059] step 1, sludge pretreatment|[0060] Fully soaking the dehydrated sludge in pure water for 1h, then pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, and then crushing and grinding the dehydrated sludge, and sieving the crushed and ground dehydrated sludge with a 80-mesh sieve for storage.|[0061] And 2, preparing a solution.|[0062] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0063] Step 3, sludge hydrothermal carbon preparation|[0064] 0.5g of pretreated sludge powder, 1g of ferric nitrate, 1.625g of lanthanum nitrate and 0.0218g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, added with potassium hydroxide to adjust the pH to 11-12, aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 200 ℃ and the reaction time is 11h. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0065] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0066] 0.05g of biochar was placed in a 100mL beaker containing 20mL of 200mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M NaOH, and then the mixture was shaken in a water bath shaker at 25.+ -. 0.5 ℃ for 12 hours at 120 rpm.|[0067] Example 5|[0068] The embodiment provides a preparation method of lanthanum-modified magnetic sludge hydrothermal carbon applied to removing phosphorus in water, which is shown in fig. 1. The preparation method comprises the following specific steps:|[0069] step 1, sludge pretreatment|[0070] Soaking dehydrated sludge in pure water for 2 hours, pre-freezing in a freeze dryer, vacuumizing for 1-2 days until the dehydrated sludge is completely dried, crushing and grinding the dehydrated sludge, and sieving with a 80-mesh sieve for storage.|[0071] And 2, preparing a solution.|[0072] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0073] Step 3, sludge hydrothermal carbon preparation|[0074] 0.5g of pretreated sludge powder, 1g of ferric sulfate, 2.4526g of lanthanum chloride and 0.04g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, added with potassium hydroxide to adjust the pH to 11-12, aged and stirred for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 200 ℃ and the reaction time is 10.5h. And after the reaction is finished, washing and suction-filtering the obtained product with pure water and ethanol for more than 3 times in turn until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon.|[0075] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the embodiment is applied to removing phosphorus in water, and comprises the following steps:|[0076] 0.05g of biochar was placed in a 100mL beaker containing 20mL of 100 (or 200) mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and then the mixture was shaken in a water bath at 25.+ -. 0.5 ℃ for 12h at 120 rpm.|[0077] Comparative example 1|[0078] In comparison with example 1, the procedure was as in example 1 except that the sludge used in this comparative example was dehydrated sludge (the water content of dehydrated sludge was 74.8%). The preparation method comprises the following specific steps:|[0079] and 1, preparing a solution.|[0080] A 6M potassium hydroxide solution was prepared for pH adjustment.|[0081] Step 2, sludge hydrothermal carbon preparation|[0082] 1.9841g of dehydrated sludge, 1g of ferric chloride, 1.8147g of lanthanum chloride and 0.0326g of ascorbic acid are added into pure water, mixed and stirred for 30 minutes, potassium hydroxide is added to adjust the pH to 11-12, and stirring is carried out for 15 minutes. Then transferring the mixture into a 100ml hydrothermal kettle, wherein the hydrothermal reaction conditions are as follows: the reaction temperature is 200 ℃ and the reaction time is 10 hours. Washing and suction-filtering the obtained product with pure water and ethanol in turn for more than 3 times after the reaction is completed until the filtered water is clear, and drying the retentate at a temperature below 65 ℃ to obtain the lanthanum modified magnetic sludge hydrothermal carbon|[0083] The lanthanum-modified magnetic sludge hydrothermal carbon prepared in the comparative example is applied to removing phosphorus in water, and comprises the following steps:|[0084] 0.05g of biochar was placed in a 100mL beaker containing 20mL of 100 (or 200) mg/L phosphate solution, the initial pH was adjusted to 7.0.+ -. 0.2 by addition of 2M HCl, and then the mixture was shaken in a water bath at 25.+ -. 0.5 ℃ for 12h at 120 rpm.|[0085] To further verify the effectiveness of the lanthanum-modified magnetic sludge hydrothermal charcoal prepared in the present invention, using example 1 and comparative example 1 as examples, 0.45 μm syringe filter was used to filter after adsorption was completed, and 0.5mL of solution was used to determine the phosphorus concentration of the terminated supernatant by molybdenum-antimony spectrophotometry. The experiments were performed in three parallel groups and the specific data are shown in table 1.|[0086] TABLE 1 total phosphorus concentration of initial solution and adsorption stop serum|[0087] |[0088] From the table, the freeze-drying pretreatment can obviously improve the adsorption performance of the sludge hydrothermal carbon, and the maximum adsorption quantity of the sludge hydrothermal carbon is 56.08mg/g. The preparation process of the invention not only can effectively recycle the sludge, but also can effectively remove the phosphorus in the water, thereby realizing the common treatment of sewage and sludge. Meanwhile, the lanthanum modified magnetic sludge hydrothermal carbon achieving adsorption balance can be used as a slow-release phosphate fertilizer.|[0089] While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the following claims be interpreted as including the preferred embodiments and all such alterations and modifications as fall within the scope of the invention.|[0090] It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof. Family Number|(103975415)|103975415|Abstract|(CN115744901B B)|The invention discloses lanthanum - modified magnetic sludge hydrothermal carbon , a preparation method thereof and application of the lanthanum - modified magnetic sludge hydrothermal carbon in removal of phosphorus in water , and belongs to the technical field of sludge recycling and water treatment . The method for preparing the lanthanum - modified magnetic sludge hydrothermal carbon comprises the following steps : soaking and cleaning sludge in water to remove impurities , performing freezing pore - forming and vacuum drying , and crushing and sieving to obtain pretreated sludge ; taking ascorbic acid as a reducing agent , adding the pretreated sludge , an iron source and a lanthanum source , uniformly mixing to obtain a mixed solution , adjusting the pH value of the mixed solution to 11-12, and carrying out hydrothermal carbonization reaction to obtain the lanthanum modified magnetic sludge hydrothermal carbon . The lanthanum modified magnetic sludge hydrothermal carbon is prepared through one - step hydrothermal carbonization , has good adsorption performance and can be used for removing phosphorus in water . |IPC codes|(CN115744901B B)|B01J - 020/20 |C01B - 032/324 |C01B - 032/348 |Title|(CN115744901 A)|Lanthanum - modified magnetic sludge hydrothermal carbon , preparation method thereof and application of lanthanum - modified magnetic sludge hydrothermal carbon in removal of phosphorus in water | Chemical engineering|Environmental technology|Materials, metallurgy Y02W-010/40 Y02W-010/40 B01J-020/20|C01B-032/324|C01B-032/348|C02F-001/28|C02F-001/68|C02F-101/10 B01J-020/20|C01B-032/324|C01B-032/348|C02F-001/28|C02F-001/68|C02F-101/10 CN114632495|CN113145073|CN113145074|CN113145075|CN112023878|CN110694583|CN105107493|US20110030586 CN114632495 100523451 WHO=Examiner SELF=N|CN113145073 95313929 WHO=Examiner SELF=N|CN113145074 95313928 WHO=Examiner SELF=N|CN113145075 95337913 WHO=Examiner SELF=N|CN112023878 91785609 WHO=Examiner SELF=N|CN110694583 87356977 WHO=Examiner SELF=N|CN105107493 71566113 WHO=Examiner SELF=N|US20110030586 44308232 WHO=Examiner SELF=N CN105107493; CN110694583; CN112023878; CN113145073; CN113145074; CN113145075; CN114632495; US20110030586 GRANTED (CN115744901)|GRANTED ALIVE (CN115744901)|ALIVE (CN115744901)|LEGAL DETAILS FOR CN115744901|Actual or expected expiration date=2042-12-02|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-12-02|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211535515|Application date=2022-12-02|Standardized application number=2022CN-1535515|Event publication date=2023-03-07|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115744901|Publication stage code=A|Publication date=2023-03-07|Standardized publication number=CN115744901|Event publication date=2023-03-07|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-03-24|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-01-23|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN115744901|Publication stage code=B|Publication date=2024-01-23|Standardized publication number=CN115744901B|Event publication date=2024-01-23|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN115744901)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoR9wuC5P6c7ZBj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000071166118&ekey=2012&xpn=CN115744901B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=PnXxDBP7iOkIOVaglbR2YrmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN115744901)|CN|(CN115744901)|CN (CN115744901)|NAME=ZHONGYUAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN|(CN115744901)|NAME=ZHONGYUAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN115744901)|NAME=LIANG JING;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223|(CN115744901)|NAME=LIANG JING;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223 (CN115744901)|NAME=GONG WEIJIN|NAME=HUANG LEI|NAME=GUO LINA|NAME=LIU YUE|NAME=ZHOU ZIZHEN|NAME=ZHAO FUWANG|(CN115744901)|NAME=GONG WEIJIN|NAME=HUANG LEI|NAME=GUO LINA|NAME=LIU YUE|NAME=ZHOU ZIZHEN|NAME=ZHAO FUWANG 0 1 Titre: (CN115744901)|Lanthanum modified magnetic sludge hydrothermal carbon, preparation method thereof and application thereof in removing phosphorus in water Résumé: (CN115744901)|The invention discloses lanthanum-modified magnetic sludge hydrothermal carbon, a preparation method thereof and application of the lanthanum-modified magnetic sludge hydrothermal carbon in removal of phosphorus in water, and belongs to the technical field of sludge recycling and water treatment. The method for preparing the lanthanum-modified magnetic sludge hydrothermal carbon comprises the following steps: soaking and cleaning sludge in water to remove impurities, performing freezing pore-forming and vacuum drying, and crushing and sieving to obtain pretreated sludge; taking ascorbic acid as a reducing agent, adding the pretreated sludge, an iron source and a lanthanum source, uniformly mixing to obtain a mixed solution, adjusting the pH value of the mixed solution to 11-12, and carrying out hydrothermal carbonization reaction to obtain the lanthanum modified magnetic sludge hydrothermal carbon. The lanthanum modified magnetic sludge hydrothermal carbon is prepared through one-step hydrothermal carbonization, has good adsorption performance and can be used for removing phosphorus in water. 46 Abstract gpt-4o-mini no The article focuses on the preparation and application of lanthanum-modified magnetic sludge for phosphorus removal in water, which does not relate to accelerated weathering or CO₂ capture.
48 CN202210294069 CN202210294069 CN114656969 100599682 CN114656969 A 2022-06-24 [CN114656969] 2022-03-24 2022-03-24 2022-06-24 (CN114656969)|2024-05-17 (CN114656969)|Method for carrying out carbon transaction by using agricultural biomass carbonization device (CN114656969)|The invention discloses a method for carbon trading by using an agricultural biomass carbonizing device. The method belongs to the field of energy conservation and emission reduction, and comprises the steps of new energy carbonized biomass carbon sequestration, biomass carbon returning and carbon emission reduction, carbon integration and carbon transaction. After agricultural biomass is harvested, under solar energy supply, the biomass is crushed by a straw crusher and is conveyed to a trough type solar carbonization pipe through a conveying belt, nitrogen protection gas is started, and the biomass is carbonized at a high temperature. In the whole process, the PLC control system regulates and controls a carbonization program through a temperature sensor and an oxygen sensor in the carbonization tube; the biological carbon can be directly returned to the field after being cooled, so that the fertilizer efficiency is improved, the soil structure is improved, and the local carbon emission of the farmland is reduced; the biomass carbon is integrated based on the carbon sequestration amount after biomass carbonization and the carbon emission reduction potential after the biochar is returned to the field, so that the integrated biomass carbon is brought into a carbon trading platform. NANJING UNIVERSITY OF INFORMATION SCIENCE & TECHNOLOGY (CN114656969)|NANJING UNIVERSITY OF INFORMATION SCIENCE & TECHNOLOGY ([CN]) SHI WENQING|ZHOU JIE|LIU BOYI|ZHU LIN|WANG JIAYI|XING RAN|ZHANG XINZHI (CN114656969)|SHI WENQING|ZHOU JIE|LIU BOYI|ZHU LIN|WANG JIAYI|XING RAN|ZHANG XINZHI (CN114656969)|CAO KUN;NANJING SUGAO PATENT & TRADEMARK FIRM|Reg. Nb: 32204 (CN114656969)|The agricultural biomass is carbonized into biological carbon, not only can permanently store carbon dioxide fixed from the atmosphere, but also can be used as a soil conditioner to adjust the soil structure, reduce the background carbon emission of farmlands and realize the dual carbon fixation and emission reduction effects; however, in the traditional biological carbon preparation process, a large amount of fossil energy needs to be input or biomass needs to be combusted for energy supply, so that the carbon sequestration efficiency is greatly reduced; meanwhile, although the yield of agricultural biomass is high every year and the carbon sequestration potential is huge, the biomass is distributed in a scattered manner, and the basal individuals lack participation power due to lack of an effective mode, so that the large-scale production is difficult to realize.| (CN114656969)|1. A device for carbonizing agricultural biomass is characterized by comprising a solar power generation system (1-1), a storage battery (1-2), an electric lead (1-3), a straw pulverizer (2-1), a feeding hole (2-2), a discharging hole (2-3), a motor (2-4), a conveying belt (3-1), a reflecting plate (4-1), a heat collection carbonization tube (4-2), a solar tracking function support (4-3), a biological carbon collection container (5-1) and a protective gas storage steel cylinder and a gas conveying pipe (6-1); the solar power generation system (1-1) comprises a supporting rod, a solar panel is arranged at the top end of the supporting rod, a storage battery (1-2) is arranged at the middle lower end of the supporting rod, and the solar panel is connected with the storage battery (1-2) through a wired line.| (CN114656969)|The invention discloses a method for performing carbon transaction by using a carbonized agricultural biomass device.|The invention relates to a device for carbonizing agricultural biomass, which comprises a solar power generation system 1-1, a storage battery 1-2, an electric lead 1-3, a straw pulverizer 2-1, a feeding port 2-2, a discharging port 2-3, a motor 2-4, a conveying belt 3-1, a reflecting plate 4-1, a heat collection carbonization tube 4-2, a solar tracking function support 4-3, a biological carbon collection container 5-1, a protective gas storage steel cylinder and a gas conveying pipe 6-1;|The purpose of the invention is as follows: the invention aims to provide a method for carrying out carbon transaction by using a carbonized agricultural biomass device, in particular to a new energy carbonized agricultural biomass device and a method for realizing carbon transaction thereof, which not only realize high-efficiency carbon fixation, but also integrate the carbon deposition and differentiation in the process into a carbon platform to realize carbon transaction.| (CN114656969)|AGRICULTURAL BIOMASS(100,8)|CARBON TRANSACTION(100,8)|CARBONIZED AGRICULTURAL BIOMASS(98,7)|STRAW PULVERIZER(54,5)|CHARRING AGRICULTURAL BIOMASS(46,1)|CONVEYING BELT(41,10)|SOLAR TRACKING(38,4)|CARBONIZATION AGRICULTURAL BIOMASS(38,2)|CARBON ACCUMULATION DIFFERENTIATION(37,2)|CARBON COLLECTION CONTAINER(30,6)|STRAW CRUSHER(30,6)|ENERGY CARBONIZATION BIOMASS(30,1)|HEAT COLLECTION CARBONIZATION TUBE(27,8)|BIOMASS CARBONIZATION(25,3)|REALIZING CARBON TRANSACTION(24,3)|FOSSIL ENERGY(24,1)|STEEL CYLINDER(22,10)|DISCHARGING PORT(22,1)|REFLECTING PLATE(19,5)|CARBON TRANSACTION PLATFORM(19,3)|DISCHARGING HOLE(19,2)|CARBON PLATFORM(19,1)|CHARRING PIPE(19,1)|FEED PORT(19,1)|HEAT COLLECTION CARBONIZATION PIPE(19,1)|FARMLAND(18,3)|ELECTRICAL LEAD(17,4)|DOUBLE CARBON FIXATION(17,1)|FEED HOLE(16,2)|FERTILIZER(16,1)|SOLAR POWER GENERATION(15,8)|CARBON SEQUESTRATION(14,10)|DIFFERENTIATION(14,2)|CARBON CREDIT(14,1)|NITROGEN GAS PROTECTION(14,1)|GAS STORAGE PROTECTION(13,10)|BIOMASS(13,9)|CARBON CONTAINER COLLECTION(13,2)|SUPPORT ROD(12,3)|STORE CARBON DIOXIDE(12,1)|STORAGE BATTERY(11,7)|CARBON FIXATION(11,5)|SOIL CONDITIONER(11,5)|CONVEYER BELT(9,7)|EMISSION REDUCTION(9,5)|PYROLYSIS(9,3)|SOLAR PANEL(9,3)|REFLECTOR(9,2)|GROOVE TYPE SOLAR CARBONIZATION(9,1)|REDUCING LOCAL CARBON EMISSION(9,1)|ENERGY CONSERVATION(7,2)|SOLAR CARBONIZATION TUBE(7,2)|CARBON PREPARATION(7,1)|ENERGY CARBONIZATION AGRICULTURAL BIOMASS(7,1)|MOTOR LEAD(6,3)|ROTATING SHAFT BELT(6,3)|STORAGE BATTERY LEAD(6,3)|WIRED LINE(6,3)|OXYGEN SENSOR(5,2)|UNIT MASS(5,2)|BIOCHAR COLLECTING CONTAINER(5,1)|COMPREHENSIVE CARBONIZATION(5,1)|ENERGY SUPPLY(5,1)|RETURNING CROP STRAW(5,1)|CARBON DIOXIDE(4,8)|CONNECTED ELECTRIC LEAD(4,5)|SOLAR TRACKING SYSTEM(4,3)|AUTOMATIC CONVEYING EQUIPMENT(4,2)|SOLAR ENERGY TRACKER(4,2)|AGRICULTURAL BIOMASS EQUIPMENT(4,1)|BIOCHAR COLLECTION VESSEL(4,1)|BIOCHAR TON(4,1)|CARBOMORPHISM PIPE(4,1)|CARBON SEQUESTRATION POPULARIZATION(4,1)|GROOVE SOLAR CARBONIZED TUBE(4,1)|MASS PRODUCTION(4,1)|RESOURCE FARMER(4,1)|SOIL STRUCTURE(4,1)|SOLAR TRACKER(4,1)|CARBON EXCHANGE(3,2)|FIXING CARBON(3,2)|SUPPORT FRAME(3,2)|TEMPERATURE SENSOR(3,2)|BIOMASS MODULE(3,1)|CARBOMORPHISM SWITCH(3,1)|CARBONIZATION GAS PROTECTION(3,1)|INEVITABLE REQUIREMENT(3,1)|NATIONAL CARBON TRADING PLATFORM(3,1)|CARBON ACCUMULATION(2,1)|CARBON DEPOSITION DIFFERENTIATION MODE(2,1)|CARBON NEUTRALIZATION(2,1)|CARBON TRADING PROFIT(2,1)|DEEP CARBON SEQUESTRATION(2,1)|ECONOMIC BENEFIT(2,1)|ENERGY CARBONIZATION EQUIPMENT(2,1)|HEAT COLLECTING CARBONIZATION TUBE(2,1)|HIGH EFFICIENCY CARBON FIXATION(2,1)| (CN114656969)|1. A device for carbonizing agricultural biomass is characterized by comprising a solar power generation system (1-1), a storage battery (1-2), an electric lead (1-3), a straw pulverizer (2-1), a feeding hole (2-2), a discharging hole (2-3), a motor (2-4), a conveying belt (3-1), a reflecting plate (4-1), a heat collection carbonization tube (4-2), a solar tracking function support (4-3), a biological carbon collection container (5-1) and a protective gas storage steel cylinder and a gas conveying pipe (6-1);|the solar power generation system (1-1) comprises a supporting rod, a solar panel is arranged at the top end of the supporting rod, a storage battery (1-2) is arranged at the middle lower end of the supporting rod, and the solar panel is connected with the storage battery (1-2) through a wired line.|2. A carbonization agricultural biomass device according to claim 1, characterized in that the feed inlet (2-2) is opened at the side of the straw crusher (2-1) facing the solar power generation system (1-1), the discharge outlet (2-3) is opened at the side of the straw crusher (2-1) facing the reflector (4-1), the first rotating shaft is installed on the straw crusher (2-1), and two support frames are also installed on the straw crusher (2-1);|a second rotating shaft matched with the first rotating shaft is arranged on the motor (2-4), and a rotating shaft belt is sleeved on the first rotating shaft and the second rotating shaft;|a third rotating shaft is further arranged on the second rotating shaft, a fourth rotating shaft is arranged on one side of the second rotating shaft, and a conveying belt (3-1) is sleeved on the third rotating shaft and the fourth rotating shaft.|3. A charring agricultural biomass device according to claim 1, wherein the reflecting plate (4-1) is arranged at the other end of the discharging port (2-3), the heat collecting charring pipe (4-2) is arranged on the reflecting plate (4-1), and the solar tracking function bracket (4-3) is arranged on the outer wall of the reflecting plate (4-1);|a fifth rotating shaft is arranged on the fourth rotating shaft, a sixth rotating shaft is arranged at the other end close to the reflector (4-1), and a second conveyor belt is sleeved on the fifth rotating shaft and the sixth rotating shaft and faces the reflector (4-1);|a biological carbon collecting container (5-1) is arranged at one side close to the sixth rotating shaft;|and a protective gas storage steel cylinder and a gas conveying pipe (6-1) are also arranged on one side of the heat collection carbonization pipe (4-2) facing the fourth rotating shaft.|4. A carbonized agricultural biomass device according to claim 1,|a storage battery lead connecting point is arranged on the storage battery (1-2), a motor lead connecting point is arranged on the motor, and a heat collection carbonization pipe lead connecting point is arranged on the heat collection carbonization pipe (4-2) and close to the protective gas storage steel cylinder and the gas conveying pipe (6-1);|the lead connecting point of the storage battery is connected with the lead connecting point of the motor through one connected electric lead (1-3), and the lead connecting point of the storage battery is connected with the lead connecting point of the heat collection carbonization tube through the other connected electric lead (1-3).|5. A method for carbon trading using a carbonized agricultural biomass device according to claims 1-4, characterized by the following specific operating steps:|(1) the system comprises a starting straw pulverizer (2-1), a conveying belt (3-1), a PLC control system, a solar power generation system and a solar tracking system of a heat collection carbonization tube;|(2) putting the biomass into a straw crusher (2-1), and conveying the crushed biomass to a heat collection carbonization pipe (4-2) for pyrolysis through a conveyor belt (3-1);|(3) after pyrolysis of the biomass is completed in the heat collection carbonization tube (4-2), the biomass is conveyed into the biological carbon collection container (5-1);|(4) cooling the biochar to normal temperature for future use and returning to the field;|(5) the carbon integral is calculated according to the following formula:|Carbon credit=M x C+M x CE|wherein M is the mass of the biochar, C is the carbon content in the biochar, and CE is the reduction capability of the biochar in unit mass on the background carbon emission of the farmland;|(6) open an account for the carbon transaction and use the carbon credits. (CN114656969)|TECHNICAL FIELD|[0001] The invention belongs to agricultural biomass negative carbon resource utilization in the field of energy conservation and emission reduction, relates to a method for carrying out carbon transaction by using a carbonized agricultural biomass device, and particularly relates to new energy carbonized agricultural biomass equipment and a method for realizing carbon transaction by using the same.|BACKGROUND ART|[0002] With the excessive use of fossil fuels and the like, a large amount of carbon dioxide is discharged, and the concentration of atmospheric carbon dioxide increases year by year, so that the obvious greenhouse effect and global warming are caused; carbon peaking and carbon neutralization are inevitable requirements for promoting high-quality development of economy and society.|[0003] The biomass is rich in carbon because of the photosynthesis of crops in the growth process to absorb a large amount of carbon dioxide, and the effective treatment can realize carbon sequestration; at present, the biological carbon sequestration technology is listed as one of the subjects of preferential development in the environmental field; and the technology of returning crop straws to the field and fixing carbon is listed as one of important technical modes of reducing emission and fixing carbon in agricultural rural areas.|[0004] The agricultural biomass is carbonized into biological carbon, not only can permanently store carbon dioxide fixed from the atmosphere, but also can be used as a soil conditioner to adjust the soil structure, reduce the background carbon emission of farmlands and realize the dual carbon fixation and emission reduction effects; however, in the traditional biological carbon preparation process, a large amount of fossil energy needs to be input or biomass needs to be combusted for energy supply, so that the carbon sequestration efficiency is greatly reduced; meanwhile, although the yield of agricultural biomass is high every year and the carbon sequestration potential is huge, the biomass is distributed in a scattered manner, and the basal individuals lack participation power due to lack of an effective mode, so that the large-scale production is difficult to realize.|DISCLOSURE|Disclosure of Invention|[0005] The purpose of the invention is as follows: the invention aims to provide a method for carrying out carbon transaction by using a carbonized agricultural biomass device, in particular to a new energy carbonized agricultural biomass device and a method for realizing carbon transaction thereof, which not only realize high-efficiency carbon fixation, but also integrate the carbon deposition and differentiation in the process into a carbon platform to realize carbon transaction. The new energy carbonization method established by the invention not only improves the carbon sequestration efficiency, but also improves the participation power of basal layer individuals by the proposed carbon deposition differentiation mode, thereby being beneficial to scale production.|[0006] The technical scheme is as follows: the invention relates to a device for carbonizing agricultural biomass, which comprises a solar power generation system (1-1), a storage battery (1-2), an electric lead (1-3), a straw pulverizer (2-1), a feeding hole (2-2), a discharging hole (2-3), a motor (2-4), a conveying belt (3-1), a reflecting plate (4-1), a heat collection carbonization tube (4-2), a solar tracking function support (4-3), a biological carbon collection container (5-1) and a protective gas storage steel cylinder and a gas conveying pipe (6-1);|[0007] the solar power generation system (1-1) comprises a supporting rod, a solar panel is arranged at the top end of the supporting rod, a storage battery (1-2) is arranged at the middle lower end of the supporting rod, and the solar panel is connected with the storage battery (1-2) through a wired line.|[0008] Further, the feeding hole (2-2) is formed in one side, facing the solar power generation system (1-1), of the straw crusher (2-1), the discharging hole (2-3) is formed in one side, facing the light reflecting plate (4-1), of the straw crusher (2-1), a first rotating shaft is arranged on the straw crusher (2-1), and two supporting frames are further arranged on the straw crusher (2-1);|[0009] a second rotating shaft matched with the first rotating shaft is arranged on the motor (2-4), and a rotating shaft belt is sleeved on the first rotating shaft and the second rotating shaft;|[0010] a third rotating shaft is further arranged on the second rotating shaft, a fourth rotating shaft is arranged on one side of the second rotating shaft, and a conveying belt (3-1) is sleeved on the third rotating shaft and the fourth rotating shaft.|[0011] Further, the reflector (4-1) is arranged at the other end of the discharge hole (2-3), the heat collecting carbonization tube (4-2) is arranged on the reflector (4-1), and the solar tracking function bracket (4-3) is arranged on the outer wall of the reflector (4-1);|[0012] a fifth rotating shaft is arranged on the fourth rotating shaft, a sixth rotating shaft is arranged at the other end close to the reflector (4-1), and a second conveyor belt is sleeved on the fifth rotating shaft and the sixth rotating shaft and faces the reflector (4-1);|[0013] a biological carbon collecting container (5-1) is arranged at one side close to the sixth rotating shaft;|[0014] and a protective gas storage steel cylinder and a gas conveying pipe (6-1) are also arranged on one side of the heat collection carbonization pipe (4-2) facing the fourth rotating shaft.|[0015] Furthermore, a storage battery lead connecting point is arranged on the storage battery (1-2), a motor lead connecting point is arranged on the motor, and a heat collection carbonization pipe lead connecting point is arranged on the heat collection carbonization pipe (4-2) and close to the protective gas storage steel cylinder and the gas conveying pipe (6-1);|[0016] the lead connecting point of the storage battery is connected with the lead connecting point of the motor through one connected electric lead (1-3), and the lead connecting point of the storage battery is connected with the lead connecting point of the heat collection carbonization tube through the other connected electric lead (1-3).|[0017] Further, a method for carrying out carbon transaction by using a carbonized agricultural biomass device comprises the following specific operation steps:|[0018] (1) the system comprises a starting straw pulverizer (2-1), a conveying belt (3-1), a PLC control system, a solar power generation system and a solar tracking system of a heat collection carbonization tube;|[0019] (2) the biomass is put into a straw crusher (2-1), and the crushed biomass is conveyed to a heat collection carbonization tube (4-2) by a conveyor belt (3-1) for pyrolysis;|[0020] (3) after pyrolysis of the biomass is completed in the heat collection carbonization tube (4-2), the biomass is conveyed into the biological carbon collection container (5-1);|[0021] (4) cooling the biochar to normal temperature for future use and returning to the field;|[0022] (5) the carbon integral is calculated according to the following formula:|[0023] Carbon credit=M x C+M x CE|[0024] wherein M is the biological carbon mass (Kg), C is the carbon content (%) in the biological carbon, and CE is the biological carbon per unit mass for farmlandBackground carbon reduction Capacity (Kg CO)2-eq/Kg biochar);|[0025] (6) making a personal account opening at a carbon exchange;|[0026] (7) and carrying out market trading on the carbon credits to obtain benefits.|[0027] Has the advantages that: compared with the prior art, the invention has the characteristics that: 1. the invention realizes double deep carbon fixation; the new energy carbonized biomass realizes direct carbon sequestration, and can indirectly reduce the background carbon emission of the farmland after being used as a soil conditioner; 2. the invention realizes carbon transaction; carbon points are generated in the resource utilization process of the agricultural biomass, so that carbon trading profit is realized, the participation enthusiasm of basic level individuals is promoted, and the large-scale carbon sequestration popularization and application are promoted.|DRAWINGS DESCRIPTION|[0028] FIG. 1 is a schematic structural view of biomass carbonization according to the invention;|[0029] FIG. 2 is a schematic comparison of carbon abatement effect in an embodiment of the present invention with a conventional process;|[0030] FIG. 3 is a schematic illustration of a biomass implementing carbon trading in an embodiment of the invention;|[0031] in the figure, 1-1 is a solar power generation system, 1-2 is a storage battery, and 1-3 is an electric lead;|[0032] 2-1 is a straw crusher, 2-2 is a feed inlet, 2-3 is a discharge outlet, and 2-4 is a motor;|[0033] 3-1 is a conveyor belt;|[0034] 4-1 is a reflecting plate, 4-2 is a heat collecting carbonization tube, and 4-3 is a solar tracking function bracket;|[0035] 5-1 is a biochar collection vessel; 6-1 is a protective gas storage steel cylinder and a gas pipe.|INVENTION MODE|Detailed Description|[0036] The invention is further described with reference to the following figures and examples.|[0037] The invention relates to a device for carbonizing agricultural biomass, which comprises a solar power generation system 1-1, a storage battery 1-2, an electric lead 1-3, a straw pulverizer 2-1, a feeding port 2-2, a discharging port 2-3, a motor 2-4, a conveying belt 3-1, a reflecting plate 4-1, a heat collection carbonization tube 4-2, a solar tracking function support 4-3, a biological carbon collection container 5-1, a protective gas storage steel cylinder and a gas conveying pipe 6-1;|[0038] the solar power generation system 1-1 comprises a support rod, a solar panel is arranged at the top end of the support rod, a storage battery 1-2 is arranged at the middle lower end of the support rod, and the solar panel is connected with the storage battery 1-2 through a wired line.|[0039] Further, the feed inlet 2-2 is arranged on one side of the straw pulverizer 2-1 facing the solar power generation system 1-1, the discharge outlet 2-3 is arranged on one side of the straw pulverizer 2-1 facing the reflector 4-1, a first rotating shaft is arranged on the straw pulverizer 2-1, and two support frames are arranged on the straw pulverizer 2-1;|[0040] a second rotating shaft matched with the first rotating shaft is arranged on the motor 2-4, and a rotating shaft belt is sleeved on the first rotating shaft and the second rotating shaft;|[0041] a third rotating shaft is further arranged on the second rotating shaft, a fourth rotating shaft is arranged on one side of the second rotating shaft, and a conveying belt 3-1 is sleeved on the third rotating shaft and the fourth rotating shaft.|[0042] Further, the reflector 4-1 is arranged at the other end of the discharge port 2-3, the heat collection carbonization tube 4-2 is arranged on the reflector 4-1, and the solar tracking function support 4-3 is arranged on the outer wall of the reflector 4-1;|[0043] a fifth rotating shaft is arranged on the fourth rotating shaft, a sixth rotating shaft is also arranged at the other end close to the reflecting plate 4-1, and a second conveying belt is sleeved on the fifth rotating shaft and the sixth rotating shaft and faces the reflecting plate 4-1;|[0044] a biochar collecting container 5-1 is arranged on one side close to the rotating shaft six;|[0045] and a protective gas storage steel cylinder and a gas conveying pipe 6-1 are also arranged on one side of the heat collection carbonization pipe 4-2 facing the fourth rotating shaft.|[0046] Furthermore, a storage battery lead connecting point is arranged on the storage battery 1-2, a motor lead connecting point is arranged on the motor, and a heat collection carbonization pipe lead connecting point is arranged on the heat collection carbonization pipe 4-2 and close to the protective gas storage steel cylinder and the gas conveying pipe 6-1;|[0047] the lead connecting point of the storage battery is connected to the lead connecting point of the motor through one connected electric lead 1-3, and the lead connecting point of the storage battery is connected to the lead connecting point of the heat collection carbonization tube through the other connected electric lead 1-3.|[0048] Further, a method for performing carbon transaction by using a carbonized agricultural biomass device comprises the following specific operation steps:|[0049] (1) starting a straw crusher 2-1, a conveyor belt 3-1, a PLC control system, a solar power generation system and a solar tracking system of a heat collection carbonization tube;|[0050] (2) putting the biomass into a straw crusher 2-1, and conveying the crushed biomass to a heat collection carbonization tube 4-2 by a conveyor belt 3-1 for pyrolysis;|[0051] (3) after pyrolysis of the biomass is completed in the heat collection carbonization tube 4-2, the biomass is conveyed into the biological carbon collection container 5-1;|[0052] (4) cooling the biochar to normal temperature for future use and returning to the field;|[0053] (5) the carbon integral is calculated according to the following formula:|[0054] Carbon credit=M x C+M x CE|[0055] wherein M is the biological carbon mass (Kg), C is the carbon content (%) in the biological carbon, and CE is the reduction capability (Kg CO) of the biological carbon of unit mass to the background carbon emission of the farmland2-eq/Kg biochar);|[0056] (6) making a personal account at the carbon exchange;|[0057] (7) and carrying out market trading on the carbon credits to obtain benefits.|[0058] Specifically, the agricultural biomass is prepared into the biomass charcoal soil conditioner by using new energy such as solar energy and the like, the carbon is directly stored and the background carbon emission of a farmland is reduced, the deep carbon sequestration and emission reduction is realized, and the carbon deposition in the process is differentiated and brought into a carbon transaction platform; the method comprises the steps of biomass carbonization by new energy, carbon returning and carbon emission reduction of the biomass, carbon accumulation and differentiation and carbon transaction; the new energy carbonized biomass module mainly comprises 2-1 parts of automatic conveying equipment, a groove type solar carbonized tube (a heat collection carbonized tube 4-2) and a PLC control system; the biomass carbon returning is to use the prepared biological carbon as a soil conditioner, improve the soil structure and reduce the background carbon emission of the farmland; the carbon accumulation differentiation and carbon transaction is to quantify the carbon fixation and emission reduction capability in the biomass carbonization and returning process, convert the carbon fixation and emission reduction capability into carbon integrals, bring the carbon integrals into a carbon transaction platform and generate economic benefit; the energy sources of the straw pulverizer 2-1 and the automatic transmission equipment are a solar power generation system 1-1; the groove type solar carbonization tube comprises a parabolic mirror surface, an atmosphere heat collecting tube, a solar tracker, a protective gas storage container and the like.|[0059] Optionally, the new energy may be non-fossil energy such as wind energy, hydroelectric energy, and the like|[0060] Further, the agricultural biomass comprises crop straws which are easy to carbonize of wheat, corn, rice and soybean.|[0061] Furthermore, solar energy trackers are arranged on the solar panel and the groove type solar carbonization tube, so that solar energy can be obtained at the maximum efficiency.|[0062] Furthermore, PLC control system is connected with temperature sensor, oxygen sensor, the electricity in the solar energy carbomorphism pipe assists carbomorphism switch, solar energy tracker to and protection gas steel bottle solenoid valve, can realize intelligent operation.|[0063] Further, when the solar carbonization tube reaches a certain temperature, the temperature sensor transmits information to the PLC control system, and the angle of the solar carbonization tube is adjusted to realize temperature control and heat preservation.|[0064] Further, when the temperature rising speed of the solar carbonization tube is slow or the temperature does not reach the required temperature, the temperature sensor transmits information to the PLC control system, and the solar electric auxiliary heating system is started.|[0065] Furthermore, when the oxygen concentration of the solar carbonization tube exceeds the standard, the PLC control system regulates and controls the electromagnetic valve of the protector, and the input quantity of the protective gas is increased.|[0066] Further, the carbonization protective gas is nitrogen inert gas and is stored by a high-pressure steel cylinder.|[0067] Furthermore, the automatic conveying equipment can resist high temperature, and can realize continuous conveying of biomass and output of biochar.|[0068] Optionally, the straw pulverizer 2-1 and the conveying device use the same motor 2-4, but need to be provided with a differential speed regulation and control system.|[0069] Optionally, the straw pulverizer 2-1 and the conveying device use different motors 2-4.|[0070] Further, the carbon integration is the sum of the carbon dioxide equivalent of the sequestered carbon and the carbon dioxide equivalent of the carbon emission cut after returning to the field.|[0071] Furthermore, the carbon integration trading platform faces all biological carbon-negative carbon resource farmers, can be in village domain level or regional level, and can be finally brought into a national carbon trading platform to realize carbon trading.|[0072] The embodiment provides a new energy carbonization agricultural biomass device and a method for realizing carbon transaction thereof.|[0073] 1 ton of biomass is carbonized by new energy carbonization equipment, the yield of the biochar is about 65 percent, the carbon content is 95 percent, and the direct carbon sequestration is realized by 0.62 ton, which is 12.4 percent higher than that of the traditional fossil fuel. The equivalent of carbon dioxide is 2.27 tons.|[0074] After the biochar is returned to the field as a soil conditioner, the soil structure is improved, and each ton of biochar can indirectly reduce the CH of the field4、CO2、N2O greenhouse gas emission of 0.027 ton CO2-eq(CO2+25CH4+298N2O)。|[0075] After comprehensive carbonization, direct carbon sealing storage and returning to the field, indirect carbon emission reduction is carried out, and the carbon integral is calculated according to the following formula, wherein the total carbon of each ton of biomass is reduced by 2.297 tons.|[0076] Carbon credit=M x C+M x CE|[0077] Wherein M is the biological carbon mass (Kg), C is the carbon content (%) in the biological carbon, and CE is the reduction capability (Kg CO) of the biological carbon of unit mass to the background carbon emission of the farmland2-eq/Kg biochar);|[0078] and (4) carrying out individual account opening in a carbon exchange, and carrying out market transaction on the carbon credits to obtain benefits.|[0079] The above is only a preferred embodiment of the present invention, and the protection scope of the present invention is not limited to the above-mentioned embodiments, and all technical solutions belonging to the idea of the present invention belong to the protection scope of the present invention. It should be noted that modifications and embellishments within the scope of the invention may be made by those skilled in the art without departing from the principle of the invention. (CN114656969)|TECHNICAL FIELD|[0001] The invention belongs to agricultural biomass negative carbon resource utilization in the field of energy conservation and emission reduction, relates to a method for carrying out carbon transaction by using a carbonized agricultural biomass device, and particularly relates to new energy carbonized agricultural biomass equipment and a method for realizing carbon transaction by using the same.|BACKGROUND ART|[0002] With the excessive use of fossil fuels and the like, a large amount of carbon dioxide is discharged, and the concentration of atmospheric carbon dioxide increases year by year, so that the obvious greenhouse effect and global warming are caused; carbon peaking and carbon neutralization are inevitable requirements for promoting high-quality development of economy and society.|[0003] The biomass is rich in carbon because of the photosynthesis of crops in the growth process to absorb a large amount of carbon dioxide, and the effective treatment can realize carbon sequestration; at present, the biological carbon sequestration technology is listed as one of the subjects of preferential development in the environmental field; and the technology of returning crop straws to the field and fixing carbon is listed as one of important technical modes of reducing emission and fixing carbon in agricultural rural areas.|[0004] The agricultural biomass is carbonized into biological carbon, not only can permanently store carbon dioxide fixed from the atmosphere, but also can be used as a soil conditioner to adjust the soil structure, reduce the background carbon emission of farmlands and realize the dual carbon fixation and emission reduction effects; however, in the traditional biological carbon preparation process, a large amount of fossil energy needs to be input or biomass needs to be combusted for energy supply, so that the carbon sequestration efficiency is greatly reduced; meanwhile, although the yield of agricultural biomass is high every year and the carbon sequestration potential is huge, the biomass is distributed in a scattered manner, and the basal individuals lack participation power due to lack of an effective mode, so that the large-scale production is difficult to realize.|DISCLOSURE|Disclosure of Invention|[0005] The purpose of the invention is as follows: the invention aims to provide a method for carrying out carbon transaction by using a carbonized agricultural biomass device, in particular to a new energy carbonized agricultural biomass device and a method for realizing carbon transaction thereof, which not only realize high-efficiency carbon fixation, but also integrate the carbon deposition and differentiation in the process into a carbon platform to realize carbon transaction. The new energy carbonization method established by the invention not only improves the carbon sequestration efficiency, but also improves the participation power of basal layer individuals by the proposed carbon deposition differentiation mode, thereby being beneficial to scale production.|[0006] The technical scheme is as follows: the invention relates to a device for carbonizing agricultural biomass, which comprises a solar power generation system (1-1), a storage battery (1-2), an electric lead (1-3), a straw pulverizer (2-1), a feeding hole (2-2), a discharging hole (2-3), a motor (2-4), a conveying belt (3-1), a reflecting plate (4-1), a heat collection carbonization tube (4-2), a solar tracking function support (4-3), a biological carbon collection container (5-1) and a protective gas storage steel cylinder and a gas conveying pipe (6-1);|[0007] the solar power generation system (1-1) comprises a supporting rod, a solar panel is arranged at the top end of the supporting rod, a storage battery (1-2) is arranged at the middle lower end of the supporting rod, and the solar panel is connected with the storage battery (1-2) through a wired line.|[0008] Further, the feeding hole (2-2) is formed in one side, facing the solar power generation system (1-1), of the straw crusher (2-1), the discharging hole (2-3) is formed in one side, facing the light reflecting plate (4-1), of the straw crusher (2-1), a first rotating shaft is arranged on the straw crusher (2-1), and two supporting frames are further arranged on the straw crusher (2-1);|[0009] a second rotating shaft matched with the first rotating shaft is arranged on the motor (2-4), and a rotating shaft belt is sleeved on the first rotating shaft and the second rotating shaft;|[0010] a third rotating shaft is further arranged on the second rotating shaft, a fourth rotating shaft is arranged on one side of the second rotating shaft, and a conveying belt (3-1) is sleeved on the third rotating shaft and the fourth rotating shaft.|[0011] Further, the reflector (4-1) is arranged at the other end of the discharge hole (2-3), the heat collecting carbonization tube (4-2) is arranged on the reflector (4-1), and the solar tracking function bracket (4-3) is arranged on the outer wall of the reflector (4-1);|[0012] a fifth rotating shaft is arranged on the fourth rotating shaft, a sixth rotating shaft is arranged at the other end close to the reflector (4-1), and a second conveyor belt is sleeved on the fifth rotating shaft and the sixth rotating shaft and faces the reflector (4-1);|[0013] a biological carbon collecting container (5-1) is arranged at one side close to the sixth rotating shaft;|[0014] and a protective gas storage steel cylinder and a gas conveying pipe (6-1) are also arranged on one side of the heat collection carbonization pipe (4-2) facing the fourth rotating shaft.|[0015] Furthermore, a storage battery lead connecting point is arranged on the storage battery (1-2), a motor lead connecting point is arranged on the motor, and a heat collection carbonization pipe lead connecting point is arranged on the heat collection carbonization pipe (4-2) and close to the protective gas storage steel cylinder and the gas conveying pipe (6-1);|[0016] the lead connecting point of the storage battery is connected with the lead connecting point of the motor through one connected electric lead (1-3), and the lead connecting point of the storage battery is connected with the lead connecting point of the heat collection carbonization tube through the other connected electric lead (1-3).|[0017] Further, a method for carrying out carbon transaction by using a carbonized agricultural biomass device comprises the following specific operation steps:|[0018] (1) the system comprises a starting straw pulverizer (2-1), a conveying belt (3-1), a PLC control system, a solar power generation system and a solar tracking system of a heat collection carbonization tube;|[0019] (2) the biomass is put into a straw crusher (2-1), and the crushed biomass is conveyed to a heat collection carbonization tube (4-2) by a conveyor belt (3-1) for pyrolysis;|[0020] (3) after pyrolysis of the biomass is completed in the heat collection carbonization tube (4-2), the biomass is conveyed into the biological carbon collection container (5-1);|[0021] (4) cooling the biochar to normal temperature for future use and returning to the field;|[0022] (5) the carbon integral is calculated according to the following formula:|[0023] Carbon credit=M x C+M x CE|[0024] wherein M is the biological carbon mass (Kg), C is the carbon content (%) in the biological carbon, and CE is the biological carbon per unit mass for farmlandBackground carbon reduction Capacity (Kg CO)2-eq/Kg biochar);|[0025] (6) making a personal account opening at a carbon exchange;|[0026] (7) and carrying out market trading on the carbon credits to obtain benefits.|[0027] Has the advantages that: compared with the prior art, the invention has the characteristics that: 1. the invention realizes double deep carbon fixation; the new energy carbonized biomass realizes direct carbon sequestration, and can indirectly reduce the background carbon emission of the farmland after being used as a soil conditioner; 2. the invention realizes carbon transaction; carbon points are generated in the resource utilization process of the agricultural biomass, so that carbon trading profit is realized, the participation enthusiasm of basic level individuals is promoted, and the large-scale carbon sequestration popularization and application are promoted.|DRAWINGS DESCRIPTION|[0028] FIG. 1 is a schematic structural view of biomass carbonization according to the invention;|[0029] FIG. 2 is a schematic comparison of carbon abatement effect in an embodiment of the present invention with a conventional process;|[0030] FIG. 3 is a schematic illustration of a biomass implementing carbon trading in an embodiment of the invention;|[0031] in the figure, 1-1 is a solar power generation system, 1-2 is a storage battery, and 1-3 is an electric lead;|[0032] 2-1 is a straw crusher, 2-2 is a feed inlet, 2-3 is a discharge outlet, and 2-4 is a motor;|[0033] 3-1 is a conveyor belt;|[0034] 4-1 is a reflecting plate, 4-2 is a heat collecting carbonization tube, and 4-3 is a solar tracking function bracket;|[0035] 5-1 is a biochar collection vessel; 6-1 is a protective gas storage steel cylinder and a gas pipe.|INVENTION MODE|Detailed Description|[0036] The invention is further described with reference to the following figures and examples.|[0037] The invention relates to a device for carbonizing agricultural biomass, which comprises a solar power generation system 1-1, a storage battery 1-2, an electric lead 1-3, a straw pulverizer 2-1, a feeding port 2-2, a discharging port 2-3, a motor 2-4, a conveying belt 3-1, a reflecting plate 4-1, a heat collection carbonization tube 4-2, a solar tracking function support 4-3, a biological carbon collection container 5-1, a protective gas storage steel cylinder and a gas conveying pipe 6-1;|[0038] the solar power generation system 1-1 comprises a support rod, a solar panel is arranged at the top end of the support rod, a storage battery 1-2 is arranged at the middle lower end of the support rod, and the solar panel is connected with the storage battery 1-2 through a wired line.|[0039] Further, the feed inlet 2-2 is arranged on one side of the straw pulverizer 2-1 facing the solar power generation system 1-1, the discharge outlet 2-3 is arranged on one side of the straw pulverizer 2-1 facing the reflector 4-1, a first rotating shaft is arranged on the straw pulverizer 2-1, and two support frames are arranged on the straw pulverizer 2-1;|[0040] a second rotating shaft matched with the first rotating shaft is arranged on the motor 2-4, and a rotating shaft belt is sleeved on the first rotating shaft and the second rotating shaft;|[0041] a third rotating shaft is further arranged on the second rotating shaft, a fourth rotating shaft is arranged on one side of the second rotating shaft, and a conveying belt 3-1 is sleeved on the third rotating shaft and the fourth rotating shaft.|[0042] Further, the reflector 4-1 is arranged at the other end of the discharge port 2-3, the heat collection carbonization tube 4-2 is arranged on the reflector 4-1, and the solar tracking function support 4-3 is arranged on the outer wall of the reflector 4-1;|[0043] a fifth rotating shaft is arranged on the fourth rotating shaft, a sixth rotating shaft is also arranged at the other end close to the reflecting plate 4-1, and a second conveying belt is sleeved on the fifth rotating shaft and the sixth rotating shaft and faces the reflecting plate 4-1;|[0044] a biochar collecting container 5-1 is arranged on one side close to the rotating shaft six;|[0045] and a protective gas storage steel cylinder and a gas conveying pipe 6-1 are also arranged on one side of the heat collection carbonization pipe 4-2 facing the fourth rotating shaft.|[0046] Furthermore, a storage battery lead connecting point is arranged on the storage battery 1-2, a motor lead connecting point is arranged on the motor, and a heat collection carbonization pipe lead connecting point is arranged on the heat collection carbonization pipe 4-2 and close to the protective gas storage steel cylinder and the gas conveying pipe 6-1;|[0047] the lead connecting point of the storage battery is connected to the lead connecting point of the motor through one connected electric lead 1-3, and the lead connecting point of the storage battery is connected to the lead connecting point of the heat collection carbonization tube through the other connected electric lead 1-3.|[0048] Further, a method for performing carbon transaction by using a carbonized agricultural biomass device comprises the following specific operation steps:|[0049] (1) starting a straw crusher 2-1, a conveyor belt 3-1, a PLC control system, a solar power generation system and a solar tracking system of a heat collection carbonization tube;|[0050] (2) putting the biomass into a straw crusher 2-1, and conveying the crushed biomass to a heat collection carbonization tube 4-2 by a conveyor belt 3-1 for pyrolysis;|[0051] (3) after pyrolysis of the biomass is completed in the heat collection carbonization tube 4-2, the biomass is conveyed into the biological carbon collection container 5-1;|[0052] (4) cooling the biochar to normal temperature for future use and returning to the field;|[0053] (5) the carbon integral is calculated according to the following formula:|[0054] Carbon credit=M x C+M x CE|[0055] wherein M is the biological carbon mass (Kg), C is the carbon content (%) in the biological carbon, and CE is the reduction capability (Kg CO) of the biological carbon of unit mass to the background carbon emission of the farmland2-eq/Kg biochar);|[0056] (6) making a personal account at the carbon exchange;|[0057] (7) and carrying out market trading on the carbon credits to obtain benefits.|[0058] Specifically, the agricultural biomass is prepared into the biomass charcoal soil conditioner by using new energy such as solar energy and the like, the carbon is directly stored and the background carbon emission of a farmland is reduced, the deep carbon sequestration and emission reduction is realized, and the carbon deposition in the process is differentiated and brought into a carbon transaction platform; the method comprises the steps of biomass carbonization by new energy, carbon returning and carbon emission reduction of the biomass, carbon accumulation and differentiation and carbon transaction; the new energy carbonized biomass module mainly comprises 2-1 parts of automatic conveying equipment, a groove type solar carbonized tube (a heat collection carbonized tube 4-2) and a PLC control system; the biomass carbon returning is to use the prepared biological carbon as a soil conditioner, improve the soil structure and reduce the background carbon emission of the farmland; the carbon accumulation differentiation and carbon transaction is to quantify the carbon fixation and emission reduction capability in the biomass carbonization and returning process, convert the carbon fixation and emission reduction capability into carbon integrals, bring the carbon integrals into a carbon transaction platform and generate economic benefit; the energy sources of the straw pulverizer 2-1 and the automatic transmission equipment are a solar power generation system 1-1; the groove type solar carbonization tube comprises a parabolic mirror surface, an atmosphere heat collecting tube, a solar tracker, a protective gas storage container and the like.|[0059] Optionally, the new energy may be non-fossil energy such as wind energy, hydroelectric energy, and the like|[0060] Further, the agricultural biomass comprises crop straws which are easy to carbonize of wheat, corn, rice and soybean.|[0061] Furthermore, solar energy trackers are arranged on the solar panel and the groove type solar carbonization tube, so that solar energy can be obtained at the maximum efficiency.|[0062] Furthermore, PLC control system is connected with temperature sensor, oxygen sensor, the electricity in the solar energy carbomorphism pipe assists carbomorphism switch, solar energy tracker to and protection gas steel bottle solenoid valve, can realize intelligent operation.|[0063] Further, when the solar carbonization tube reaches a certain temperature, the temperature sensor transmits information to the PLC control system, and the angle of the solar carbonization tube is adjusted to realize temperature control and heat preservation.|[0064] Further, when the temperature rising speed of the solar carbonization tube is slow or the temperature does not reach the required temperature, the temperature sensor transmits information to the PLC control system, and the solar electric auxiliary heating system is started.|[0065] Furthermore, when the oxygen concentration of the solar carbonization tube exceeds the standard, the PLC control system regulates and controls the electromagnetic valve of the protector, and the input quantity of the protective gas is increased.|[0066] Further, the carbonization protective gas is nitrogen inert gas and is stored by a high-pressure steel cylinder.|[0067] Furthermore, the automatic conveying equipment can resist high temperature, and can realize continuous conveying of biomass and output of biochar.|[0068] Optionally, the straw pulverizer 2-1 and the conveying device use the same motor 2-4, but need to be provided with a differential speed regulation and control system.|[0069] Optionally, the straw pulverizer 2-1 and the conveying device use different motors 2-4.|[0070] Further, the carbon integration is the sum of the carbon dioxide equivalent of the sequestered carbon and the carbon dioxide equivalent of the carbon emission cut after returning to the field.|[0071] Furthermore, the carbon integration trading platform faces all biological carbon-negative carbon resource farmers, can be in village domain level or regional level, and can be finally brought into a national carbon trading platform to realize carbon trading.|[0072] The embodiment provides a new energy carbonization agricultural biomass device and a method for realizing carbon transaction thereof.|[0073] 1 ton of biomass is carbonized by new energy carbonization equipment, the yield of the biochar is about 65 percent, the carbon content is 95 percent, and the direct carbon sequestration is realized by 0.62 ton, which is 12.4 percent higher than that of the traditional fossil fuel. The equivalent of carbon dioxide is 2.27 tons.|[0074] After the biochar is returned to the field as a soil conditioner, the soil structure is improved, and each ton of biochar can indirectly reduce the CH of the field4、CO2、N2O greenhouse gas emission of 0.027 ton CO2-eq(CO2+25CH4+298N2O)。|[0075] After comprehensive carbonization, direct carbon sealing storage and returning to the field, indirect carbon emission reduction is carried out, and the carbon integral is calculated according to the following formula, wherein the total carbon of each ton of biomass is reduced by 2.297 tons.|[0076] Carbon credit=M x C+M x CE|[0077] Wherein M is the biological carbon mass (Kg), C is the carbon content (%) in the biological carbon, and CE is the reduction capability (Kg CO) of the biological carbon of unit mass to the background carbon emission of the farmland2-eq/Kg biochar);|[0078] and (4) carrying out individual account opening in a carbon exchange, and carrying out market transaction on the carbon credits to obtain benefits.|[0079] The above is only a preferred embodiment of the present invention, and the protection scope of the present invention is not limited to the above-mentioned embodiments, and all technical solutions belonging to the idea of the present invention belong to the protection scope of the present invention. It should be noted that modifications and embellishments within the scope of the invention may be made by those skilled in the art without departing from the principle of the invention. Family Number|(100599682)|100599682|Abstract|(CN114656969 A)|The invention discloses a method for carbon trading by using an agricultural biomass carbonizing device . The method belongs to the field of energy conservation and emission reduction , and comprises the steps of new energy carbonized biomass carbon sequestration , biomass carbon returning and carbon emission reduction , carbon integration and carbon transaction . After agricultural biomass is harvested , under solar energy supply , the biomass is crushed by a straw crusher and is conveyed to a trough type solar carbonization pipe through a conveying belt , nitrogen protection gas is started , and the biomass is carbonized at a high temperature . In the whole process , the PLC control system regulates and controls a carbonization program through a temperature sensor and an oxygen sensor in the carbonization tube ; the biological carbon can be directly returned to the field after being cooled , so that the fertilizer efficiency is improved , the soil structure is improved , and the local carbon emission of the farmland is reduced ; the biomass carbon is integrated based on the carbon sequestration amount after biomass carbonization and the carbon emission reduction potential after the biochar is returned to the field , so that the integrated biomass carbon is brought into a carbon trading platform . |CPC codes|(CN114656969 A)|C01B - 032/05 |IPC codes|(CN114656969 A)|C01B - 032/05 | Basic materials chemistry|IT methods for management|Materials, metallurgy C01B-032/05|C09K-017/02|C09K-2101/00|G06Q-040/04|G06Q-050/02|G06Q-050/06 C01B-032/05|C09K-017/02|C09K-2101/00|G06Q-040/04|G06Q-050/02|G06Q-050/06 C01B-032/05|C09K-017/02|C09K-101/00|G06Q-040/04|G06Q-050/02|G06Q-050/06 C01B-032/05|C09K-017/02|C09K-101/00|G06Q-040/04|G06Q-050/02|G06Q-050/06 CN115374386 CN115374386 102692428 WHO=Examiner SELF=Y CAT=A CN214708863U|CN110819365|CN114996356|CN114065488|CN215048660U|CN112430469|CN105295972|US20170051221|CN203944250U|US20130341175|CN101787293 CN214708863U 97058597 WHO=Examiner SELF=N CAT=Y|CN110819365 87717982 WHO=Examiner SELF=N CAT=Y|CN114996356 101622359 WHO=Examiner SELF=N CAT=T|CN114065488 98774859 WHO=Examiner SELF=N CAT=A|CN215048660U 97516710 WHO=Examiner SELF=N CAT=A|CN112430469 92970636 WHO=Examiner SELF=N CAT=A|CN105295972 72154952 WHO=Examiner SELF=N CAT=A|US20170051221 70567176 WHO=Examiner SELF=N CAT=A|CN203944250U 67948733 WHO=Examiner SELF=Y CAT=A|US20130341175 61235805 WHO=Examiner SELF=N CAT=A|CN101787293 7037785 WHO=Examiner SELF=N CAT=A 刘航;: &quot;碳普惠制:理论分析、经验借鉴与框架设计&quot; (Cat. A)|唐剑武;叶属峰;陈雪初;杨华蕾;孙晓红;王法明;温泉;陈少波;: &quot;海岸带蓝碳的科学概念、研究方法以及在生态恢复中的应用&quot; (Cat. A)|靳国良: &quot;碳交易机制的普惠制创新&quot; (Cat. Y) CN101787293; US20130341175; CN203944250U; CN105295972; US20170051221; CN110819365; CN112430469; CN214708863U; CN215048660U; CN114065488; CN114996356 REVOKED (CN114656969)|REVOKED DEAD (CN114656969)|DEAD (CN114656969)|LEGAL DETAILS FOR CN114656969|Actual or expected expiration date=2024-05-17|Legal state=DEAD|Status=REVOKED|Event publication date=2022-03-24|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210294069|Application date=2022-03-24|Standardized application number=2022CN-0294069|Event publication date=2022-06-24|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114656969|Publication stage code=A|Publication date=2022-06-24|Standardized publication number=CN114656969|Event publication date=2022-06-24|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-07-12|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-05-17|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRIfeSG3Vqa8Ffn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000063462467&ekey=2353&xpn=CN114656969&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=fmckmJCnKx1PUxNLR3fC3JNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN114656969)|CN (CN114656969)|NAME=NANJING UNIVERSITY OF INFORMATION SCIENCE & TECHNOLOGY , COUNTRY=CN (CN114656969)|NAME=CAO KUN;NANJING SUGAO PATENT & TRADEMARK FIRM , REG=32204 (CN114656969)|NAME=SHI WENQING|NAME=ZHOU JIE|NAME=LIU BOYI|NAME=ZHU LIN|NAME=WANG JIAYI|NAME=XING RAN|NAME=ZHANG XINZHI 0 1 Titre: (CN114656969)|Method for carrying out carbon transaction by using agricultural biomass carbonization device Résumé: (CN114656969)|The invention discloses a method for carbon trading by using an agricultural biomass carbonizing device. The method belongs to the field of energy conservation and emission reduction, and comprises the steps of new energy carbonized biomass carbon sequestration, biomass carbon returning and carbon emission reduction, carbon integration and carbon transaction. After agricultural biomass is harvested, under solar energy supply, the biomass is crushed by a straw crusher and is conveyed to a trough type solar carbonization pipe through a conveying belt, nitrogen protection gas is started, and the biomass is carbonized at a high temperature. In the whole process, the PLC control system regulates and controls a carbonization program through a temperature sensor and an oxygen sensor in the carbonization tube; the biological carbon can be directly returned to the field after being cooled, so that the fertilizer efficiency is improved, the soil structure is improved, and the local carbon emission of the farmland is reduced; the biomass carbon is integrated based on the carbon sequestration amount after biomass carbonization and the carbon emission reduction potential after the biochar is returned to the field, so that the integrated biomass carbon is brought into a carbon trading platform. 47 Abstract gpt-4o-mini no The article focuses on carbon trading and biomass carbonization, which does not involve the accelerated weathering of minerals or CO₂ capture through mineral carbonation.
49 CN202411977823 CN202411977823 CN119607861 113778323 CN119607861 A 2025-03-14 [CN119607861] 2024-12-31 2024-12-31 2025-03-14 (CN119607861)|2044-12-31 (CN119607861)|Carbon capture and storage system and carbon capture and storage method (CN119607861)|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture and storage system and a carbon capture and storage method.The carbon capture and storage system comprises a waste gas absorption unit, an amine liquid circulation unit, a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence; the system further comprises a limestone slurry pulping and filling unit; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. The carbon capture and storage method is a brand-new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer, the method has the advantages that the carbon capturing and storing process is short, high-pressure and low-temperature high-energy-consumption equipment does not need to be used, the captured carbon dioxide gas does not need to be stored and transported at low temperature, energy consumption can be reduced, the carbon sequestration cost is saved, and the carbon sequestration efficiency is improved. The carbon dioxide escape phenomenon in the storage and transportation process can be avoided, and the carbon sequestration efficiency is improved. SINOTECH ENERGY|ZHONGTAI CARBON SHANGHAI ENVIRONMENTAL PROTECTION SCIENCE & TECHNOLOGY (CN119607861)|SINOTECH ENERGY CO., LTD. ([CN])|ZHONGTAI CARBON SHANGHAI ENVIRONMENTAL PROTECTION SCIENCE AND TECH LIMITED COMPANY WEI YING|HE WEI (CN119607861)|WEI YING|HE WEI (CN119607861)|Compared with the prior art, the invention has the advantages that: (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved.| (CN119607861)|1. The carbon capturing and storing system is characterized by comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit, a carbon fixation and sealing unit and a limestone slurry pulping and filling unit; The waste gas absorption unit comprises a temperature reduction tower and an absorption tower, wherein the upper part of the temperature reduction tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reduction tower is communicated with the absorption tower, a seawater spraying device is arranged in the temperature reduction tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reduction tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through a water conveying pipeline, the bottom of the temperature reduction tower is also provided with a seawater outlet, the upper end in the absorption tower is provided with a lean amine liquid spraying device, and the top of the absorption tower is provided with an exhaust port; The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. | (CN119607861)|The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.Disclosure of InventionThe invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.|The invention relates to the technical field of flue gas treatment, in particular to a carbon capturing and storing system and a carbon capturing and storing method, comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit and a carbon fixing and sealing unit which are sequentially communicated; the device also comprises a limestone slurry pulping and filling unit which is communicated with the carbon dioxide gas salinization unit.| (CN119607861)|DESORPTION TOWER(100,39)|CARBON CAPTURE(100,17)|CARBON(100,15)|CARBON CAPTURE STORAGE(100,13)|STORAGE SYSTEM(100,13)|CARBON CAPTURE STORAGE SYSTEM(100,11)|LIMESTONE SLURRY POND(87,21)|CARBONIZATION TANK(85,38)|ABSORPTION TOWER(84,60)|LIMESTONE SLURRY(74,32)|SLAG DISCHARGE(72,6)|AMINE DECARBURIZATION STORAGE(62,4)|REGENERATING GAS COOLER(57,14)|ORGANIC AMINE DECARBURIZATION STORAGE(54,4)|CONVEYING PIPELINE(51,9)|DECARBURIZATION STORAGE(51,4)|SLURRY POND(49,21)|SEAWATER PUMP(49,9)|GAS SALINIZATION(48,8)|FLUE GAS CONVEYING PIPELINE(44,9)|ORGANIC AMINE DECARBURIZATION(44,1)|LEAN AMINE LIQUID(42,27)|AMINE DECARBURIZATION(42,1)|CARBONIZATION TANK BOTTOM(38,12)|AMINE LIQUID(37,54)|COMPRESSOR(35,26)|CARBON DIOXIDE GAS SALINIZATION(35,8)|CONVEYING LIMESTONE SLURRY RESIDUE(34,2)|BUBBLE DISTRIBUTOR(33,8)|LEAN LIQUID COOLER(32,6)|SEAWATER(31,27)|COOLED LEAN AMINE(31,4)|LEAN RICH LIQUID INLET(30,2)|GAS SALIFYING(29,2)|MANPOWER(29,2)|WATER CONVEYING PIPELINE(29,2)|ENHANCED ROCK(29,1)|RICH AMINE LIQUID(28,19)|CONVEYING LIMESTONE POWDER(28,2)|OVERLONG CARBON CAPTURE(28,1)|CARBON DIOXIDE(27,65)|TEMPERATURE REDUCTION TOWER(27,29)|AMINE LIQUID CIRCULATION(27,6)|LIMESTONE SLURRY TANK(27,4)|SEAWATER OUTLET(26,5)|CARBON DIOXIDE GAS(25,33)|LIQUID CLARIFICATION(25,12)|REBOILER(25,10)|LEAN LIQUID INLET(25,6)|RICH LIQUID HEAT EXCHANGER(25,6)|TREATING FLUE GAS(25,2)|LEAN LIQUID PUMP(24,9)|TRANSPORTATION(24,8)|LIQUEFACTION(24,3)|CARBON DIOXIDE ESCAPE(24,2)|CARBON FIXATION(23,11)|SOLUBLE CALCIUM BICARBONATE(23,7)|CARBON DIOXIDE GAS SALIFYING(23,2)|FLUE GAS(22,22)|LIQUID CIRCULATION(22,6)|FIXED CARBON FIXATION(22,1)|LEAN RICH SOLUTION(22,1)|RICH LIQUID PUMP(21,11)|RICH LIQUID INLET(21,6)|LEAN LIQUID OUTLET(21,3)|ROCK REINFORCEMENT(21,3)|LARGE MANPOWER(21,2)|GAS OUTLET(20,10)|CARBON FIXING(20,6)|CALCIUM BICARBONATE(19,14)|MIXER(19,12)|LIMESTONE(19,7)|BOOSTER FAN(19,3)|RICH LIQUID OUTLET(19,3)|DECARBURIZATION TREATMENT(19,2)|LEAN SOLUTION COOLER(19,2)|CONSUMPTION EQUIPMENT(19,1)|ACIDIC CONDITION(18,6)|SLAG DISCHARGE PUMP(18,4)|EQUIPMENT RESOURCE CONSUMPTION(18,3)|LEAN(18,2)|DEEP SEA DISCHARGE AREA(17,8)|SALTY WATER LAYER SEALING(17,2)|SEALING FLOW(17,2)|WATER FLOW PIPELINE(16,6)|HEAT EXCHANGER(15,26)|LIMESTONE SLURRY PUMP(15,6)|ORGANIC AMINE(15,4)|TRANSPORTATION(15,3)|STEAM ABSORPTION HEAT(14,3)|CARBON FIXATION COST(14,1)|BYPASS VALVE(13,8)|DISCHARGE AREA(13,8)|SUPERFINE LIMESTONE POWDER(13,3)|FLUE GAS SOURCE(12,6)|EXHAUST GAS(12,5)|CARBONIZATION TANK TOP(12,3)|DISCHARGE OUTLET(12,3)|CARBON CAPTURE SEALING(12,2)|EQUIPMENT RESOURCE(12,1)|WATER OUTLET(11,6)|BIN(11,4)|ENERGY CONSUMPTION(11,3)|LIQUID HEAT EXCHANGER(11,2)|WASTE GAS(10,25)|TEMPERATURE REDUCTION TOWER BOTTOM(10,7)|EXHAUST PORT(10,4)|AIRFLOW PIPELINE(10,3)|CARBON DIOXIDE CARBON FIXING(10,1)|CARBON FIXING COST(10,1)|STIRRER(9,7)|HIGH ENERGY CONSUMPTION(9,3)|SLURRY CONVEYING PIPELINE(9,2)|CONVEYING LIMESTONE SLURRY SLAG(9,1)|SEALING(9,1)|GENERATED CALCIUM BICARBONATE(8,3)|COMPRESSOR BOOSTER REFRIGERATOR(8,1)|MIXED LIQUID(7,6)|AIR FLOW PIPELINE(7,3)|DESLAGGING PUMP(7,3)|PH VALUE(7,2)|WASTE GAS ABSORPTION UNIT(7,2)|LIMESTONE POWDER WAREHOUSE(7,1)|ABSORPTION UNIT(6,2)|LIMESTONE SEDIMENT(6,1)|TRIETHYLENE TETRAMINE(6,1)|MIXER UPPER END(5,3)|SEAWATER SPRAY(5,1)|FORMED RICH AMINE LIQUID(4,3)|BICARBONATE ION(4,2)|FORMED LEAN AMINE SOLUTION(4,2)|INPUT END(4,2)|LEAN AMINE LIQUID SPRAY(4,1)|SIMULTANEOUSLY CONVEYING LIMESTONE POWDER(4,1)|AIR OUTLET(3,5)|CLEAN GAS(3,2)|DECARBONIZATION(3,2)|OUTPUT END(3,2)|ABSORPTION CARBON(3,1)|CARBON DIOXIDE ESCAPING PHENOMENON(3,1)| (CN119607861)|1. The carbon capturing and storing system is characterized by comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit, a carbon fixation and sealing unit and a limestone slurry pulping and filling unit;| The waste gas absorption unit comprises a temperature reduction tower and an absorption tower, wherein the upper part of the temperature reduction tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reduction tower is communicated with the absorption tower, a seawater spraying device is arranged in the temperature reduction tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reduction tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through a water conveying pipeline, the bottom of the temperature reduction tower is also provided with a seawater outlet, the upper end in the absorption tower is provided with a lean amine liquid spraying device, and the top of the absorption tower is provided with an exhaust port; | The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; | The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; | The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; | The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. |2. The carbon capture and storage system of claim 1, wherein the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an air flow pipeline, and a booster fan is arranged on the air flow pipeline between the temperature reduction tower and the absorption tower.|3. The carbon capture storage system of claim 2, wherein the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein an input end of the rich liquid pump is communicated with the bottom of the absorption tower, an output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, an input end of the lean liquid pump is communicated with the bottom of the desorption tower, and an output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.|4. A carbon capture storage system according to claim 2, wherein a pressure relief valve is disposed in the gas flow line between the gas outlet and the compressor.|5. The carbon capture and storage system according to claim 2, wherein a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.|6. A carbon capture storage system according to claim 2 wherein the bottom of the filter is in communication with a limestone slurry pond, the upper end of the filter is further provided with a gas outlet, and the gas outlet is in communication with the input of the compressor via a gas flow line.|7. A carbon capture storage method, characterized in that the carbon capture storage system according to any one of claims 1 to 6 is used for carbon capture storage, comprising the steps of:| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; | S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; | S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; | S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; | s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. |8. The carbon capture storage method of claim 7, wherein in S2, the twice cooling of the formed lean amine solution comprises cooling to 60-70 ℃ by a lean rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.|9. The carbon capture storage method of claim 7, wherein in S5 the ratio of clarified liquid to seawater is 1 (10-1000). (CN119607861)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.|BACKGROUND ART|[0002] The carbon dioxide discharged by the large amount of fossil fuels is a main cause of global warming, the carbon dioxide discharged is captured, utilized and sealed, and is one of the most effective means for realizing large-scale carbon emission reduction and coping with climate change, and at present, the carbon dioxide is captured by adopting a chemical absorption carbon capturing technology after the fossil fuels are combusted.|[0003] The method for decarbonizing and storing the organic amine is one of the most main carbon trapping technologies by a chemical absorption method, and the existing method for decarbonizing and storing the organic amine is a method for capturing and storing the carbon dioxide from the waste gas by utilizing the principle that an organic amine is in contact with the carbon-containing waste gas and is subjected to absorption reaction and then rich liquid is heated and reversibly desorbed, then the carbon dioxide is stored in a liquid tank by utilizing a method of cooling and liquefying a compressor booster refrigerator, and the liquid carbon dioxide is conveyed to underground capable of being permanently stored by transportation, so that the purpose of capturing and storing the carbon dioxide is achieved.|[0004] In the process of capturing and sealing carbon dioxide by adopting the organic amine decarburization storage method, a large amount of energy is consumed in the processes of compressing, liquefying, storing, transporting, sealing and the like of the carbon dioxide, at least 300KWh of energy is consumed per ton of compressed, liquefied and stored carbon dioxide, and in addition, the carbon dioxide is sealed in a low-temperature, high-pressure storage and high-pressure saline water layer sealing mode, so that the capturing and sealing process of the method is longer, the carbon dioxide is required to be ensured to be in a liquid state during the capturing and sealing process, and high energy is required to be consumed for keeping the liquid state of the carbon dioxide.|[0005] The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.|[0007] The technical scheme includes that the carbon capturing and storing system comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit, a carbon fixing and sealing unit and a limestone slurry pulping and filling unit, wherein the exhaust gas absorbing unit comprises a temperature reducing tower and an absorbing tower, the upper part of the temperature reducing tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reducing tower is communicated with the absorbing tower, a seawater spraying device is arranged in the temperature reducing tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reducing tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through the water conveying pipeline, the bottom of the temperature reducing tower is also provided with a seawater outlet, the upper end of the inside of the absorbing tower is provided with a lean amine liquid spraying device, and the top of the absorbing tower is provided with an exhaust port;| The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; | The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; | The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; | The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. |[0008] Preferably, the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an airflow pipeline, and a booster fan is arranged on the airflow pipeline between the temperature reduction tower and the absorption tower.|[0009] Preferably, the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein the input end of the rich liquid pump is communicated with the bottom of the absorption tower, the output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, the input end of the lean liquid pump is communicated with the bottom of the desorption tower, and the output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.|[0010] Preferably, a pressure reducing valve is arranged on the air flow pipeline between the air outlet and the compressor.|[0011] Preferably, a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.|[0012] Preferably, the bottom of the filter is communicated with the limestone slurry pond, the upper end of the filter is also provided with a gas outlet, and the gas outlet is communicated with the input end of the compressor through a gas flow pipeline.|[0013] The invention also provides a method for capturing and storing carbon by adopting the carbon capturing and storing system, which specifically comprises the following steps:| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; | S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; | S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; | S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; | s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. |[0014] Preferably, in S2, the two cooling steps of the formed lean amine solution include cooling to 60-70 ℃ by a lean-rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.|[0015] Preferably, in S5, the ratio of clarified liquid to seawater is 1 (10-1000).|[0016] Compared with the prior art, the invention has the advantages that:| (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved. |[0017] (2) The carbon capture storage system and the carbon capture storage method provided by the invention are characterized in that the carbon capture storage method is used for converting the resolved carbon dioxide gas and limestone slurry into calcium bicarbonate under an acidic condition, and the calcium bicarbonate can exist stably in the form of bicarbonate ions and calcium ions under deep sea and low temperature conditions, so that the carbon capture storage method can realize the purpose of permanently fixing carbon.|DRAWINGS DESCRIPTION|[0018] The invention is further described below with reference to the accompanying drawings and examples:| FIG. 1 is a schematic diagram of a carbon capture storage system according to the present invention; | The device comprises a temperature reduction tower, a2 absorption tower, a3 bypass valve, a 4 sea water pump, a 5 sea water outlet, a 6, an exhaust port, a7, a desorption tower, a 8, a lean-rich liquid heat exchanger, a9, a reboiler, a 10, a lean liquid cooler, a 11, a regenerated gas cooler, a 12, a compressor, a 13, a carbonization tank, a 14, an air outlet, a 15, a slag discharge pump, a 16, a filter, a 17, a mixer, a 18, a water outlet, a 19, a PH meter, a 20, a limestone slurry pond, a 21, a limestone powder warehouse, a 22, a booster fan, a 23, a rich liquid pump, a 24, a lean liquid pump, a 25, a pressure reducing valve, a 26, a bubble distributor, a 27, a stirrer, a 28, a gas outlet, a 29 and a limestone slurry pump. |INVENTION MODE|Detailed Description|[0019] The following describes the present invention in further detail with reference to specific examples:| A carbon capturing and storing system is shown in fig. 1, and comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit and a carbon fixation and sealing unit which are sequentially communicated, wherein the carbon capturing and storing system also comprises a limestone slurry pulping and filling unit, and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. |[0020] The waste gas absorption unit comprises a temperature reduction tower 1 and an absorption tower 2; the upper part of the temperature reduction tower 1 is communicated with a flue gas source through a flue gas conveying pipeline, and a bypass valve 3 is arranged on the flue gas conveying pipeline between the temperature reduction tower 1 and the flue gas source; the bypass valve 3 is opened to convey the waste gas to be decarbonized into the temperature reduction tower 1 for cooling treatment, a seawater spray device is arranged at the upper end of the interior of the temperature reduction tower 1, the seawater spray device is connected with the output end of a seawater pump 4 positioned outside the temperature reduction tower 1 through a water pipeline, the seawater is conveyed into the temperature reduction tower 1, the upper end of the temperature reduction tower 1 sprays the waste gas to the bottom of the temperature reduction tower 1 and fully contacts and mixes the waste gas conveyed into the temperature reduction tower 1 to further reduce the temperature of the waste gas, the bottom of the temperature reduction tower 1 is communicated with the absorption tower 2 and is used for conveying the waste gas subjected to the spray cooling treatment into the absorption tower 2, a seawater outlet 5 is also arranged at the bottom of the temperature reduction tower 1, a water pipeline leading to a seawater discharge area is connected at the seawater outlet 5 and is used for discharging the seawater sprayed to the bottom of the temperature reduction tower 1 into the sea, a lean amine liquid spray device is arranged at the upper end of the absorption tower 2 and is used for spraying the lean amine liquid from the upper end of the absorption tower 2 to a filler position close to the bottom of the absorption tower 2 and is fully contacted with the waste gas conveyed into the absorption tower 2, the waste gas is further reduced in temperature, the bottom of the absorption tower 2 is in contact with the waste gas is formed by the pure amine gas and the pure amine gas is discharged into the absorption tower 2 through the clean gas after the absorption tower 2 is relatively connected to the top of the absorption tower 2 through the clean gas which is relatively arranged to the top of the absorption tower 2, and the booster fan 22 is further arranged on the airflow pipeline between the temperature reduction tower 1 and the absorption tower 2 and is used for increasing the pressure of the waste gas conveyed into the absorption tower 2, increasing the flow speed and the airflow energy of the waste gas, and fully mixing the waste gas with the lean amine liquid in the absorption tower 2, so that the carbon dioxide gas in the waste gas fully contacts with the lean amine liquid and is absorbed by the lean amine liquid, and capturing the carbon dioxide gas in the waste gas is realized.|[0021] The amine liquid circulation unit comprises a desorption tower 7, a lean-rich liquid heat exchanger 8 and a reboiler 9, wherein the reboiler 9 is communicated with the desorption tower 7 and is connected to a position close to the bottom of the desorption tower 7, namely a filler, a rich liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the absorption tower 2, a rich liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the desorption tower 7 and is used for heating the rich amine liquid at the bottom of the absorption tower 2 and then conveying the rich amine liquid to the top of the desorption tower 7, a spraying device at the top of the desorption tower 7 is used for spraying the rich amine liquid close to the bottom of the desorption tower 7 from the top of the desorption tower 7, the rich amine liquid sprayed to the filler absorbs steam heat generated by the reboiler 9 and then heats and desorbs carbon dioxide to form lean amine liquid containing only a small amount of carbon dioxide, and flows to the bottom of the desorption tower 7, a lean liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the desorption tower 7, a lean liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the absorption tower 2 through a lean liquid cooler 10 and is used for cooling the lean liquid at the bottom of the absorption tower 2, and is conveyed to the top of the absorption tower 2 from the lean liquid heat exchanger 8 to the top of the absorption tower 2 through the lean liquid heat exchanger 10 and then is recycled to the absorption tower 2. In order to ensure continuous and stable mutual circulation and transportation of the rich amine liquid and the lean amine liquid formed in the absorption tower 2 and the desorption tower 7 so as to achieve the effect of recycling the organic amine liquid, the amine liquid circulation unit further comprises a rich liquid pump 23 and a lean liquid pump 24, wherein the input end of the rich liquid pump 23 is communicated with the bottom of the absorption tower 2, the output end of the rich liquid pump is communicated with the rich liquid inlet of the lean-rich liquid heat exchanger 8 and is used for pumping the rich amine liquid formed in the absorption tower 2 into the lean-rich liquid heat exchanger 8 and transporting the rich amine liquid into the desorption tower 7, and similarly, the input end of the lean liquid pump 24 is communicated with the bottom of the desorption tower 7, and the output end of the rich liquid pump 24 is communicated with the lean liquid inlet of the lean-rich liquid heat exchanger 8.|[0022] The carbon dioxide gas salinization unit comprises a regeneration gas cooler 11, a compressor 12 and a carbonization tank 13, wherein the input end of the regeneration gas cooler 11 is communicated with the top of the desorption tower 7, the output end of the regeneration gas cooler is communicated with the input end of the compressor 12, the output end of the compressor 12 is communicated with the bottom of the carbonization tank 13, carbon dioxide gas desorbed in the desorption tower 7 is cooled by the regeneration gas cooler 11, dehydrated and then flows into the compressor 12, the compressor 12 is pressurized and then is conveyed into the carbonization tank 13, and based on the rock weathering principle, the carbon dioxide gas and limestone slurry in the carbonization tank 13 are mixed and react under the acidic condition to form soluble calcium bicarbonate. In order to sufficiently mix and sufficiently react the carbon dioxide gas with the limestone slurry in the carbonization tank 13, a bubble distributor 26 and a stirrer 27 may be provided in the carbonization tank 13, the bubble distributor 26 may be connected to the output end of the compressor 12, the carbon dioxide gas supplied into the carbonization tank 13 by the compressor 12 may be separated into fine bubbles by the bubble distributor 26, the dissolution efficiency of the carbon dioxide gas in the limestone slurry may be improved, the contact ratio of the carbon dioxide gas with the limestone slurry may be increased, and the reaction efficiency may be improved, and the carbon dioxide gas and the limestone slurry in the carbonization tank 13 may be sufficiently mixed and reacted with each other by stirring by the stirrer 27, thereby further improving the conversion rate of the carbon dioxide.|[0023] The carbon sequestration unit comprises a deslagging pump 15, a filter 16 and a mixer 17, wherein the input end of the deslagging pump 15 is communicated with the bottom of the carbonization tank 13, the output end of the deslagging pump 15 is communicated with the filter 16 and is used for conveying soluble calcium bicarbonate and limestone slurry generated by the reaction at the bottom of the carbonization tank 13 into the filter 16 together for filtering, the upper end of the filter 16 is communicated with the mixer 17, the upper end of the mixer 17 is communicated with the output end of the sea water pump 4 through a water flow pipeline, the lower end of the mixer 17 is provided with a water outlet 18, the water outlet 18 is communicated with a water flow pipeline leading to a deep sea discharge area, the clarified liquid separated from the filter 16 is conveyed into the mixer 17 and is mixed with sea water from the sea water pump 4 in the mixer 17 to form mixed liquid, then the mixed liquid is discharged into the deep sea discharge area through the water flow pipeline to achieve the purpose of permanently sequestration, and a PH meter 19 is further arranged at the water outlet 18 and is used for monitoring the PH value of the mixed liquid and the sea water, and the clear liquid is discharged into the deep sea after the PH value of the clear liquid meets the requirements. The upper end of the filter 16 is also provided with a gas outlet 28, and the gas outlet 28 is communicated with the input end of the compressor 12 through a gas flow pipeline and is used for conveying the carbon dioxide gas which is conveyed into the filter 16 together with the soluble calcium bicarbonate and limestone slurry into a carbon dioxide gas salinization unit for continuous salinization.|[0024] The limestone slurry pulping and filling unit comprises a limestone slurry pond 20, wherein the upper part of the limestone slurry pond 20 is respectively communicated with a limestone powder bin 21 and the output end of a sea water pump 4, and is used for adding superfine limestone powder and sea water in the limestone powder bin 21 into the limestone slurry pond 20 together and uniformly mixing the superfine limestone powder and the sea water in the limestone slurry pond 20 to form limestone slurry, a stirrer 27 is further arranged in the limestone slurry pond 20, stirring is performed by adopting the stirrer 27 in the process of adding the limestone powder and the sea water into the limestone slurry pond 20, so that rapid uniform mixing of the limestone powder and the sea water is facilitated, the bottom of the limestone slurry pond 20 is communicated with the upper part of a carbonization tank 13 through a slurry conveying pipeline, a limestone slurry pump 29 is arranged on the slurry conveying pipeline, and the limestone slurry in the limestone slurry pond 20 is pumped into the carbonization tank 13 through the limestone slurry pump 29 to perform internal reaction. The bottom of the filter 16 is also communicated with the limestone slurry pond 20, and limestone sediment formed at the lower layer in the filter 16 is conveyed into the limestone slurry pond 20 and is used as a raw material together with superfine limestone powder to prepare limestone slurry.|[0025] The method for capturing and storing carbon by adopting the carbon capturing and storing system specifically comprises the following steps:| S1, when the waste gas needs to be decarbonized, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, seawater sprayed through a Wen Dana is fully contacted with the flue gas and absorbs heat brought by the flue gas, so that the flue gas is cooled to be within a range of 40-60 ℃, then, the waste gas flows into the absorption tower from the bottom of the absorption tower, is contacted with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, rich amine liquid and relatively pure gas are formed, and the relatively pure gas is discharged into the atmosphere from an exhaust port at the top of the absorption tower or is conveyed to a subsequent gas treatment unit. Wherein, the flue gas is conveyed into a temperature reduction tower according to the gas flow of 50-500L/h, the lean amine liquid in the absorption tower can be one of aqueous solution or mixed aqueous solution of a plurality of methyl diethanolamine, ethanolamine, triethylene tetramine and the like, and the concentration of carbon dioxide gas in the relatively pure gas is below 2.0 percent (mole percent). |[0026] S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid to the bottom from the top of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a bottom reboiler, desorbing carbon dioxide gas, forming lean amine liquid, and flowing to the bottom of the desorption tower.|[0027] S3, cooling the lean amine liquid at the bottom of the desorption tower to 60-70 ℃ through a lean-rich liquid heat exchanger, cooling to 30-45 ℃ through a lean liquid cooler, conveying the lean amine liquid to the top of the absorption tower, spraying the lean amine liquid to the bottom of the absorption tower from the top in the absorption tower, simultaneously, cooling and dewatering the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing to 4-6bar through a compressor, and conveying the carbon dioxide gas to the bottom of a carbonization tank, and then, based on the reinforced rock weathering principle, absorbing and reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, wherein the reaction equation is as follows: And conveying part of unreacted carbon dioxide gas to a compressor from an air outlet at the top of the carbonization tank, compressing and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again. |[0028] S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter according to the flow ratio of 5-100L/h for filtering to form clarified liquid and limestone slurry slag, simultaneously conveying limestone powder and seawater into a limestone slurry pond to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank according to the flow ratio of 5-100L/h.|[0029] S5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater according to the proportion of 1 (10-1000), forming mixed liquid with the pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, achieving the purpose of carbon fixation and sealing, and conveying limestone slurry slag in the filter into a limestone slurry pond for preparing limestone slurry.|[0030] Compared with the traditional carbon fixation method for sealing and storing carbon dioxide through compression, liquefaction and transportation and an underground salty water layer, the carbon capture and storage method does not need high-pressure and low-temperature high-energy equipment, low-temperature storage and transportation, saves the cost consumed in the low-temperature storage, transportation and sealing and storage processes, avoids the carbon dioxide escaping phenomenon in the transportation process, greatly shortens the carbon fixation process, and reduces the carbon fixation energy consumption. In addition, because the calcium bicarbonate exists in the form of bicarbonate ions and calcium ions in the sea water and can exist stably under deep sea and low temperature conditions, the carbon capturing and storing method can better achieve the purpose of carbon fixation and sealing.|[0031] The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement the same according to the content of the present invention, and are not intended to limit the scope of the present invention. It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it is therefore desired that the present invention be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. (CN119607861)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.|BACKGROUND ART|[0002] The carbon dioxide discharged by the large amount of fossil fuels is a main cause of global warming, the carbon dioxide discharged is captured, utilized and sealed, and is one of the most effective means for realizing large-scale carbon emission reduction and coping with climate change, and at present, the carbon dioxide is captured by adopting a chemical absorption carbon capturing technology after the fossil fuels are combusted.|[0003] The method for decarbonizing and storing the organic amine is one of the most main carbon trapping technologies by a chemical absorption method, and the existing method for decarbonizing and storing the organic amine is a method for capturing and storing the carbon dioxide from the waste gas by utilizing the principle that an organic amine is in contact with the carbon-containing waste gas and is subjected to absorption reaction and then rich liquid is heated and reversibly desorbed, then the carbon dioxide is stored in a liquid tank by utilizing a method of cooling and liquefying a compressor booster refrigerator, and the liquid carbon dioxide is conveyed to underground capable of being permanently stored by transportation, so that the purpose of capturing and storing the carbon dioxide is achieved.|[0004] In the process of capturing and sealing carbon dioxide by adopting the organic amine decarburization storage method, a large amount of energy is consumed in the processes of compressing, liquefying, storing, transporting, sealing and the like of the carbon dioxide, at least 300KWh of energy is consumed per ton of compressed, liquefied and stored carbon dioxide, and in addition, the carbon dioxide is sealed in a low-temperature, high-pressure storage and high-pressure saline water layer sealing mode, so that the capturing and sealing process of the method is longer, the carbon dioxide is required to be ensured to be in a liquid state during the capturing and sealing process, and high energy is required to be consumed for keeping the liquid state of the carbon dioxide.|[0005] The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.|[0007] The technical scheme includes that the carbon capturing and storing system comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit, a carbon fixing and sealing unit and a limestone slurry pulping and filling unit, wherein the exhaust gas absorbing unit comprises a temperature reducing tower and an absorbing tower, the upper part of the temperature reducing tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reducing tower is communicated with the absorbing tower, a seawater spraying device is arranged in the temperature reducing tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reducing tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through the water conveying pipeline, the bottom of the temperature reducing tower is also provided with a seawater outlet, the upper end of the inside of the absorbing tower is provided with a lean amine liquid spraying device, and the top of the absorbing tower is provided with an exhaust port;| The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; | The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; | The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; | The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. |[0008] Preferably, the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an airflow pipeline, and a booster fan is arranged on the airflow pipeline between the temperature reduction tower and the absorption tower.|[0009] Preferably, the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein the input end of the rich liquid pump is communicated with the bottom of the absorption tower, the output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, the input end of the lean liquid pump is communicated with the bottom of the desorption tower, and the output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.|[0010] Preferably, a pressure reducing valve is arranged on the air flow pipeline between the air outlet and the compressor.|[0011] Preferably, a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.|[0012] Preferably, the bottom of the filter is communicated with the limestone slurry pond, the upper end of the filter is also provided with a gas outlet, and the gas outlet is communicated with the input end of the compressor through a gas flow pipeline.|[0013] The invention also provides a method for capturing and storing carbon by adopting the carbon capturing and storing system, which specifically comprises the following steps:| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; | S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; | S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; | S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; | s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. |[0014] Preferably, in S2, the two cooling steps of the formed lean amine solution include cooling to 60-70 ℃ by a lean-rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.|[0015] Preferably, in S5, the ratio of clarified liquid to seawater is 1 (10-1000).|[0016] Compared with the prior art, the invention has the advantages that:| (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved. |[0017] (2) The carbon capture storage system and the carbon capture storage method provided by the invention are characterized in that the carbon capture storage method is used for converting the resolved carbon dioxide gas and limestone slurry into calcium bicarbonate under an acidic condition, and the calcium bicarbonate can exist stably in the form of bicarbonate ions and calcium ions under deep sea and low temperature conditions, so that the carbon capture storage method can realize the purpose of permanently fixing carbon.|DRAWINGS DESCRIPTION|[0018] The invention is further described below with reference to the accompanying drawings and examples:| FIG. 1 is a schematic diagram of a carbon capture storage system according to the present invention; | The device comprises a temperature reduction tower, a2 absorption tower, a3 bypass valve, a 4 sea water pump, a 5 sea water outlet, a 6, an exhaust port, a7, a desorption tower, a 8, a lean-rich liquid heat exchanger, a9, a reboiler, a 10, a lean liquid cooler, a 11, a regenerated gas cooler, a 12, a compressor, a 13, a carbonization tank, a 14, an air outlet, a 15, a slag discharge pump, a 16, a filter, a 17, a mixer, a 18, a water outlet, a 19, a PH meter, a 20, a limestone slurry pond, a 21, a limestone powder warehouse, a 22, a booster fan, a 23, a rich liquid pump, a 24, a lean liquid pump, a 25, a pressure reducing valve, a 26, a bubble distributor, a 27, a stirrer, a 28, a gas outlet, a 29 and a limestone slurry pump. |INVENTION MODE|Detailed Description|[0019] The following describes the present invention in further detail with reference to specific examples:| A carbon capturing and storing system is shown in fig. 1, and comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit and a carbon fixation and sealing unit which are sequentially communicated, wherein the carbon capturing and storing system also comprises a limestone slurry pulping and filling unit, and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. |[0020] The waste gas absorption unit comprises a temperature reduction tower 1 and an absorption tower 2; the upper part of the temperature reduction tower 1 is communicated with a flue gas source through a flue gas conveying pipeline, and a bypass valve 3 is arranged on the flue gas conveying pipeline between the temperature reduction tower 1 and the flue gas source; the bypass valve 3 is opened to convey the waste gas to be decarbonized into the temperature reduction tower 1 for cooling treatment, a seawater spray device is arranged at the upper end of the interior of the temperature reduction tower 1, the seawater spray device is connected with the output end of a seawater pump 4 positioned outside the temperature reduction tower 1 through a water pipeline, the seawater is conveyed into the temperature reduction tower 1, the upper end of the temperature reduction tower 1 sprays the waste gas to the bottom of the temperature reduction tower 1 and fully contacts and mixes the waste gas conveyed into the temperature reduction tower 1 to further reduce the temperature of the waste gas, the bottom of the temperature reduction tower 1 is communicated with the absorption tower 2 and is used for conveying the waste gas subjected to the spray cooling treatment into the absorption tower 2, a seawater outlet 5 is also arranged at the bottom of the temperature reduction tower 1, a water pipeline leading to a seawater discharge area is connected at the seawater outlet 5 and is used for discharging the seawater sprayed to the bottom of the temperature reduction tower 1 into the sea, a lean amine liquid spray device is arranged at the upper end of the absorption tower 2 and is used for spraying the lean amine liquid from the upper end of the absorption tower 2 to a filler position close to the bottom of the absorption tower 2 and is fully contacted with the waste gas conveyed into the absorption tower 2, the waste gas is further reduced in temperature, the bottom of the absorption tower 2 is in contact with the waste gas is formed by the pure amine gas and the pure amine gas is discharged into the absorption tower 2 through the clean gas after the absorption tower 2 is relatively connected to the top of the absorption tower 2 through the clean gas which is relatively arranged to the top of the absorption tower 2, and the booster fan 22 is further arranged on the airflow pipeline between the temperature reduction tower 1 and the absorption tower 2 and is used for increasing the pressure of the waste gas conveyed into the absorption tower 2, increasing the flow speed and the airflow energy of the waste gas, and fully mixing the waste gas with the lean amine liquid in the absorption tower 2, so that the carbon dioxide gas in the waste gas fully contacts with the lean amine liquid and is absorbed by the lean amine liquid, and capturing the carbon dioxide gas in the waste gas is realized.|[0021] The amine liquid circulation unit comprises a desorption tower 7, a lean-rich liquid heat exchanger 8 and a reboiler 9, wherein the reboiler 9 is communicated with the desorption tower 7 and is connected to a position close to the bottom of the desorption tower 7, namely a filler, a rich liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the absorption tower 2, a rich liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the desorption tower 7 and is used for heating the rich amine liquid at the bottom of the absorption tower 2 and then conveying the rich amine liquid to the top of the desorption tower 7, a spraying device at the top of the desorption tower 7 is used for spraying the rich amine liquid close to the bottom of the desorption tower 7 from the top of the desorption tower 7, the rich amine liquid sprayed to the filler absorbs steam heat generated by the reboiler 9 and then heats and desorbs carbon dioxide to form lean amine liquid containing only a small amount of carbon dioxide, and flows to the bottom of the desorption tower 7, a lean liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the desorption tower 7, a lean liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the absorption tower 2 through a lean liquid cooler 10 and is used for cooling the lean liquid at the bottom of the absorption tower 2, and is conveyed to the top of the absorption tower 2 from the lean liquid heat exchanger 8 to the top of the absorption tower 2 through the lean liquid heat exchanger 10 and then is recycled to the absorption tower 2. In order to ensure continuous and stable mutual circulation and transportation of the rich amine liquid and the lean amine liquid formed in the absorption tower 2 and the desorption tower 7 so as to achieve the effect of recycling the organic amine liquid, the amine liquid circulation unit further comprises a rich liquid pump 23 and a lean liquid pump 24, wherein the input end of the rich liquid pump 23 is communicated with the bottom of the absorption tower 2, the output end of the rich liquid pump is communicated with the rich liquid inlet of the lean-rich liquid heat exchanger 8 and is used for pumping the rich amine liquid formed in the absorption tower 2 into the lean-rich liquid heat exchanger 8 and transporting the rich amine liquid into the desorption tower 7, and similarly, the input end of the lean liquid pump 24 is communicated with the bottom of the desorption tower 7, and the output end of the rich liquid pump 24 is communicated with the lean liquid inlet of the lean-rich liquid heat exchanger 8.|[0022] The carbon dioxide gas salinization unit comprises a regeneration gas cooler 11, a compressor 12 and a carbonization tank 13, wherein the input end of the regeneration gas cooler 11 is communicated with the top of the desorption tower 7, the output end of the regeneration gas cooler is communicated with the input end of the compressor 12, the output end of the compressor 12 is communicated with the bottom of the carbonization tank 13, carbon dioxide gas desorbed in the desorption tower 7 is cooled by the regeneration gas cooler 11, dehydrated and then flows into the compressor 12, the compressor 12 is pressurized and then is conveyed into the carbonization tank 13, and based on the rock weathering principle, the carbon dioxide gas and limestone slurry in the carbonization tank 13 are mixed and react under the acidic condition to form soluble calcium bicarbonate. In order to sufficiently mix and sufficiently react the carbon dioxide gas with the limestone slurry in the carbonization tank 13, a bubble distributor 26 and a stirrer 27 may be provided in the carbonization tank 13, the bubble distributor 26 may be connected to the output end of the compressor 12, the carbon dioxide gas supplied into the carbonization tank 13 by the compressor 12 may be separated into fine bubbles by the bubble distributor 26, the dissolution efficiency of the carbon dioxide gas in the limestone slurry may be improved, the contact ratio of the carbon dioxide gas with the limestone slurry may be increased, and the reaction efficiency may be improved, and the carbon dioxide gas and the limestone slurry in the carbonization tank 13 may be sufficiently mixed and reacted with each other by stirring by the stirrer 27, thereby further improving the conversion rate of the carbon dioxide.|[0023] The carbon sequestration unit comprises a deslagging pump 15, a filter 16 and a mixer 17, wherein the input end of the deslagging pump 15 is communicated with the bottom of the carbonization tank 13, the output end of the deslagging pump 15 is communicated with the filter 16 and is used for conveying soluble calcium bicarbonate and limestone slurry generated by the reaction at the bottom of the carbonization tank 13 into the filter 16 together for filtering, the upper end of the filter 16 is communicated with the mixer 17, the upper end of the mixer 17 is communicated with the output end of the sea water pump 4 through a water flow pipeline, the lower end of the mixer 17 is provided with a water outlet 18, the water outlet 18 is communicated with a water flow pipeline leading to a deep sea discharge area, the clarified liquid separated from the filter 16 is conveyed into the mixer 17 and is mixed with sea water from the sea water pump 4 in the mixer 17 to form mixed liquid, then the mixed liquid is discharged into the deep sea discharge area through the water flow pipeline to achieve the purpose of permanently sequestration, and a PH meter 19 is further arranged at the water outlet 18 and is used for monitoring the PH value of the mixed liquid and the sea water, and the clear liquid is discharged into the deep sea after the PH value of the clear liquid meets the requirements. The upper end of the filter 16 is also provided with a gas outlet 28, and the gas outlet 28 is communicated with the input end of the compressor 12 through a gas flow pipeline and is used for conveying the carbon dioxide gas which is conveyed into the filter 16 together with the soluble calcium bicarbonate and limestone slurry into a carbon dioxide gas salinization unit for continuous salinization.|[0024] The limestone slurry pulping and filling unit comprises a limestone slurry pond 20, wherein the upper part of the limestone slurry pond 20 is respectively communicated with a limestone powder bin 21 and the output end of a sea water pump 4, and is used for adding superfine limestone powder and sea water in the limestone powder bin 21 into the limestone slurry pond 20 together and uniformly mixing the superfine limestone powder and the sea water in the limestone slurry pond 20 to form limestone slurry, a stirrer 27 is further arranged in the limestone slurry pond 20, stirring is performed by adopting the stirrer 27 in the process of adding the limestone powder and the sea water into the limestone slurry pond 20, so that rapid uniform mixing of the limestone powder and the sea water is facilitated, the bottom of the limestone slurry pond 20 is communicated with the upper part of a carbonization tank 13 through a slurry conveying pipeline, a limestone slurry pump 29 is arranged on the slurry conveying pipeline, and the limestone slurry in the limestone slurry pond 20 is pumped into the carbonization tank 13 through the limestone slurry pump 29 to perform internal reaction. The bottom of the filter 16 is also communicated with the limestone slurry pond 20, and limestone sediment formed at the lower layer in the filter 16 is conveyed into the limestone slurry pond 20 and is used as a raw material together with superfine limestone powder to prepare limestone slurry.|[0025] The method for capturing and storing carbon by adopting the carbon capturing and storing system specifically comprises the following steps:| S1, when the waste gas needs to be decarbonized, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, seawater sprayed through a Wen Dana is fully contacted with the flue gas and absorbs heat brought by the flue gas, so that the flue gas is cooled to be within a range of 40-60 ℃, then, the waste gas flows into the absorption tower from the bottom of the absorption tower, is contacted with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, rich amine liquid and relatively pure gas are formed, and the relatively pure gas is discharged into the atmosphere from an exhaust port at the top of the absorption tower or is conveyed to a subsequent gas treatment unit. Wherein, the flue gas is conveyed into a temperature reduction tower according to the gas flow of 50-500L/h, the lean amine liquid in the absorption tower can be one of aqueous solution or mixed aqueous solution of a plurality of methyl diethanolamine, ethanolamine, triethylene tetramine and the like, and the concentration of carbon dioxide gas in the relatively pure gas is below 2.0 percent (mole percent). |[0026] S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid to the bottom from the top of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a bottom reboiler, desorbing carbon dioxide gas, forming lean amine liquid, and flowing to the bottom of the desorption tower.|[0027] S3, cooling the lean amine liquid at the bottom of the desorption tower to 60-70 ℃ through a lean-rich liquid heat exchanger, cooling to 30-45 ℃ through a lean liquid cooler, conveying the lean amine liquid to the top of the absorption tower, spraying the lean amine liquid to the bottom of the absorption tower from the top in the absorption tower, simultaneously, cooling and dewatering the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing to 4-6bar through a compressor, and conveying the carbon dioxide gas to the bottom of a carbonization tank, and then, based on the reinforced rock weathering principle, absorbing and reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, wherein the reaction equation is as follows: And conveying part of unreacted carbon dioxide gas to a compressor from an air outlet at the top of the carbonization tank, compressing and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again. |[0028] S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter according to the flow ratio of 5-100L/h for filtering to form clarified liquid and limestone slurry slag, simultaneously conveying limestone powder and seawater into a limestone slurry pond to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank according to the flow ratio of 5-100L/h.|[0029] S5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater according to the proportion of 1 (10-1000), forming mixed liquid with the pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, achieving the purpose of carbon fixation and sealing, and conveying limestone slurry slag in the filter into a limestone slurry pond for preparing limestone slurry.|[0030] Compared with the traditional carbon fixation method for sealing and storing carbon dioxide through compression, liquefaction and transportation and an underground salty water layer, the carbon capture and storage method does not need high-pressure and low-temperature high-energy equipment, low-temperature storage and transportation, saves the cost consumed in the low-temperature storage, transportation and sealing and storage processes, avoids the carbon dioxide escaping phenomenon in the transportation process, greatly shortens the carbon fixation process, and reduces the carbon fixation energy consumption. In addition, because the calcium bicarbonate exists in the form of bicarbonate ions and calcium ions in the sea water and can exist stably under deep sea and low temperature conditions, the carbon capturing and storing method can better achieve the purpose of carbon fixation and sealing.|[0031] The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement the same according to the content of the present invention, and are not intended to limit the scope of the present invention. It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it is therefore desired that the present invention be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Family Number|(113778323)|113778323|Abstract|(CN119607861 A)|The invention relates to the technical field of flue gas treatment , in particular to a carbon capture and storage system and a carbon capture and storage method . The carbon capture and storage system comprises a waste gas absorption unit , an amine liquid circulation unit , a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence ; the system further comprises a limestone slurry pulping and filling unit ; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit . The carbon capture and storage method is a brand - new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering ; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer , the method has the advantages that the carbon capturing and storing process is short , high - pressure and low - temperature high - energy - consumption equipment does not need to be used , the captured carbon dioxide gas does not need to be stored and transported at low temperature , energy consumption can be reduced , the carbon sequestration cost is saved , and the carbon sequestration efficiency is improved . The carbon dioxide escape phenomenon in the storage and transportation process can be avoided , and the carbon sequestration efficiency is improved . |CPC codes|(CN119607861 A)|B01D - 053/62 |B01D - 053/78 |B01D - 053/80 |B01D - 053/96 |B01D - 2258/0283 |C01B - 032/55 |IPC codes|(CN119607861 A)|B01D - 053/62 |B01D - 053/78 |B01D - 053/80 |B01D - 053/96 |C01B - 032/55 | Environmental technology|Materials, metallurgy B01D-053/62|B01D-053/78|B01D-053/80|B01D-053/96|B01D-2258/0283|C01B-032/55 B01D-053/62|B01D-053/78|B01D-053/80|B01D-053/96|B01D-2258/0283|C01B-032/55 B01D-053/62|B01D-053/78|B01D-053/80|B01D-053/96|C01B-032/55 B01D-053/62|B01D-053/78|B01D-053/80|B01D-053/96|C01B-032/55 CN119838413 CN119838413 114246229 WHO=Examiner SELF=N CAT=A PENDING (CN119607861)|PENDING ALIVE (CN119607861)|ALIVE (CN119607861)|LEGAL DETAILS FOR CN119607861|Actual or expected expiration date=2044-12-31|Legal state=ALIVE|Status=PENDING|Event publication date=2024-12-31|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202411977823|Application date=2024-12-31|Standardized application number=2024CN-1977823|Event publication date=2025-03-14|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119607861|Publication stage code=A|Publication date=2025-03-14|Standardized publication number=CN119607861|Event publication date=2025-03-14|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-04-01|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN119607861)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTcM0PYETPPhlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000076748113&ekey=2056&xpn=CN119607861&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=X3YLgN33UC9MvSpo4Kvsq5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN119607861)|CN (CN119607861)|NAME=SINOTECH ENERGY CO., LTD. , COUNTRY=CN (CN119607861)|NAME=WEI YING|NAME=HE WEI 0 1 Titre: (CN119607861)|Carbon capture and storage system and carbon capture and storage method Résumé: (CN119607861)|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture and storage system and a carbon capture and storage method.The carbon capture and storage system comprises a waste gas absorption unit, an amine liquid circulation unit, a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence; the system further comprises a limestone slurry pulping and filling unit; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. The carbon capture and storage method is a brand-new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer, the method has the advantages that the carbon capturing and storing process is short, high-pressure and low-temperature high-energy-consumption equipment does not need to be used, the captured carbon dioxide gas does not need to be stored and transported at low temperature, energy consumption can be reduced, the carbon sequestration cost is saved, and the carbon sequestration efficiency is improved. The carbon dioxide escape phenomenon in the storage and transportation process can be avoided, and the carbon sequestration efficiency is improved. 49 Abstract gpt-4o-mini no The article focuses on a carbon capture and storage system related to flue gas treatment, which does not align with the topic of accelerated weathering of rocks for CO₂ sequestration.
50 CN202210008427 CN202210008427 CN116440942|CN116440942 105754646 CN116440942 B 2024-10-01 [CN116440942B]|CN116440942 A 2023-07-18 [CN116440942] 2022-01-06 2022-01-06 2024-10-01|2023-07-18 (CN116440942B)|2024-10-01 (CN116440942)|2042-01-06 (CN116440942)|Method for recycling waste catalyst (CN116440942)|The invention discloses a method for recycling a waste catalyst. The method comprises the following steps: (1) carrying out oil removal, carbon removal, crushing and screening on the waste supported hydrocracking catalyst; (2) carrying out alkali treatment by adopting an alkaline solution to obtain a molybdenum-containing aqueous solution and solid residues containing nickel, aluminum and silicon; (3) carrying out acid treatment by adopting an acid solution to obtain a nickel-containing aqueous solution and a silicon-aluminum material containing the Y-type molecular sieve; (4) adding an organic solvent and the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding an aluminum-containing acidic solution and an aluminum-containing alkaline solution, carrying out a first gelling reaction, sequentially and alternately adding the aluminum-containing acidic solution and the aluminum-containing alkaline solution, and carrying out swing gelling and aging to obtain a catalyst carrier; and (5) impregnating the catalyst carrier with a solution containing active metal components, drying, and roasting to obtain the novel hydrocracking catalyst. The hydrocracking catalyst obtained by the method is good in hydrogenation and cracking performance and has better raw material adaptability. CHINA PETROLEUM & CHEMICAL|SINOPEC DALIAN RESEARCH INSTITUTE OF PETROLEUM & PETROCHEMICALS (CN116440942)|CHINA PETROLEUM & CHEMICAL CORP. ([CN])|SINOPEC DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS CO., LTD.|(CN116440942)|CHINA PETROLEUM & CHEMICAL CORP. ([CN])|SINOPEC DALIAN RES INST PETROLEUM & PETROCHEMICALS LÜ ZHENHUI|PENG CHONG|XUE DONG|ZHU HUIHONG (CN116440942)|LÜ ZHENHUI|PENG CHONG|XUE DONG|ZHU HUIHONG|(CN116440942)|LÜ ZHENHUI|PENG CHONG|XUE DONG|ZHU HUIHONG (CN116440942)|Compared with the prior art, the invention has the following advantages:| (CN116440942)|1. A method for recycling a spent catalyst, the method comprising: (1) Degreasing and decarbonizing the waste supported hydrocracking catalyst, and then crushing and sieving; (2) Performing alkali treatment on the powder sieved in the step (1) by adopting an alkaline solution to obtain a molybdenum-containing aqueous solution and nickel-containing aluminum-silicon solid residues; (3) Acid treatment is carried out on the solid residues containing nickel, aluminum and silicon obtained in the step (2) by adopting an acid solution, so as to obtain a nickel-containing aqueous solution and a silicon-aluminum material containing a Y-type molecular sieve; (4) Adding an organic solvent and the silicon-aluminum material containing the Y molecular sieve obtained in the step (3) into a reaction kettle, stirring, adding an aluminum-containing acidic solution and an aluminum-containing alkaline solution, regulating the pH value to perform a first gel forming reaction, then sequentially and alternately adding the aluminum-containing acidic solution and the aluminum-containing alkaline solution, oscillating to form gel, and aging to obtain a catalyst carrier; (5) Impregnating the catalyst carrier obtained in the step (4) by using a solution containing an active metal component, and drying and roasting to obtain a novel hydrocracking catalyst; In the step (1), the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve. | (CN116440942)|Aiming at the defects of the prior art, the invention provides a method for recycling a waste catalyst, which takes the waste supported hydrocracking catalyst as a raw material to prepare a novel hydrocracking catalyst, the method has the characteristics of simple preparation process, high metal recovery rate, low treatment cost and the like, and the obtained hydrocracking catalyst has good hydrogenation and cracking performances and better raw material adaptability. The invention provides a method for recycling a waste catalyst, which comprises the following steps:|The invention discloses a method for recycling a waste catalyst.|The invention relates to a method for recycling a waste catalyst, in particular to a method for recycling a waste supported hydrocracking catalyst to prepare a novel hydrocracking catalyst.| (CN116440942)|RECYCLED WASTE CATALYST(100,5)|SPENT CATALYST RECYCLING(100,1)|HYDROCRACKING CATALYST(84,40)|WASTE SUPPORTED HYDROCRACKING CATALYST(56,30)|ALKALINE SOLUTION(41,17)|ACIDIC SOLUTION(39,17)|CATALYST CARRIER(33,15)|CRACKING PERFORMANCE(26,2)|ALKALI TREATMENT(25,5)|SIO MOLAR RATIO(25,2)|Y MOLECULAR SIEVE(24,18)|HYDROGENATION(24,2)|SPENT SUPPORTED HYDROCRACKING CATALYST(24,1)|POWDER GRANULARITY(23,1)|SWINGING GLUE(23,1)|MOLECULAR SIEVE(22,40)|REACTION KETTLE(22,17)|DECARBONIZATION(21,2)|SOLID RESIDUE(20,23)|AQUEOUS SOLUTION(20,10)|ORGANIC SOLVENT(20,8)|DEGREASING(20,3)|ALKALINE GLUE(20,1)|ORGANIC ALCOHOL(19,5)|ACIDIC COMPOUND(19,3)|MOLYBDENUM(18,25)|LEACHING(18,22)|CRUSHING(18,9)|COCOA APERTURE(18,1)|SIEVING(17,4)|ALKANE(16,4)|AGING CONDITION(16,3)|SODIUM METAALUMINATE SOLUTION(15,28)|ACID TREATMENT(15,4)|PORE VOLUME(15,4)|HYDROTREATMENT(15,1)|PORE DIAMETER(14,3)|CATALYST PARTICLE(14,2)|PETROLEUM ETHER(13,5)|DEOILING(13,1)|MASS CONTENT(12,12)|ALUMINOSILICATE MATERIAL(12,2)|TRIMETHYLOLETHANE(12,2)|ORGANIC MONOHYDRIC ALCOHOL(11,2)|RAW MATERIAL ADAPTABILITY(11,2)|ACID TREATMENT CONDITION(10,3)|ALUMINUM SILICON SOLID RESIDUE(10,3)|TREATMENT TEMPERATURE(10,3)|ORGANIC POLYHYDRIC ALCOHOL(10,2)|PENTAERYTHRITOL(10,2)|SWINGING TEMPERATURE(10,2)|STIRRING SPEED(10,1)|AUTOCLAVE(9,17)|ACTIVE METAL COMPONENT(9,3)|ALKENE(9,2)|AROMATIC CARBOXYLIC ACID(9,2)|EXTRACTION TEMPERATURE(9,2)|OLEFIN(9,2)|XYLITOL(9,2)|HEATING RATE(8,7)|DODECANE(8,3)|ALKALI TREATMENT CONDITION(8,2)|HEXENE(8,2)|PENTANE(8,2)|PENTENE(8,2)|REMOVING OIL(8,2)|SORBITOL(8,2)|SILICON ALUMINUM MATERIAL(7,27)|PH VALUE(7,17)|REACTION PRESSURE(7,12)|WASHING SOLUTION(7,11)|AGING PH(7,7)|REMOVING CARBON(7,3)|AMMONIUM BICARBONATE(7,2)|GLYCEROL(7,2)|PORE SIZE(7,2)|RAD MIN(7,1)|ALUMINUM SULFATE SOLUTION(6,21)|CATALYST RESIDUE(6,5)|HEXANE(6,4)|CRYSTAL NUCLEUS(6,3)|CARBONIC ACID(6,2)|EXTENSIVE UTILIZATION(6,2)|MOLYBDENUM OXIDE WEIGHT CONTENT(6,2)|SULFUROUS ACID(6,2)|UREA(6,2)|METAL RECOVERY RATE(6,1)|RECOVERY RATE(6,1)|STOPPING(5,14)|AGING TEMPERATURE(5,7)|NICKEL SILICON ALUMINUM(5,7)|MESH POWDER(5,6)|ORGANIC ACID(5,4)|HEAVY INFERIOR RAW MATERIAL(5,3)|EXTRACTING TOLUENE(5,2)|HYDROCRACKING CATALYST CARRIER SUPPORT(5,2)|NICKEL OXIDE WEIGHT CONTENT(5,2)|WASTE SUPPORTED HYDROGENATION CATALYST(5,2)|HYDROGENATION SPENT CATALYST(5,1)|ISOVOLUMETRIC IMPREGNATION(5,1)|OSCILLATION TIME(5,1)|RECOVERED WASTE HYDROCRACKING CATALYST(5,1)|TREATMENT COST(5,1)|VANADIUM PRECIPITATION TANK(5,1)|WASTE CATALYST COMPREHENSIVE UTILIZATION(5,1)|WASTE HYDROGENATION CATALYST(5,1)|MOO(4,9)|TREATMENT TIME(4,6)|NIO WEIGHT CONTENT(4,5)|AFTER ALKALI TREATMENT(4,4)|CARBON CONTENT(4,4)|ACTIVITY EVALUATION(4,2)|ALUMINUM OXIDE(4,2)|CATALYST ACTIVITY(4,2)|GLUE TIME(4,2)|N HEPTANOL(4,2)|N HEXANOL(4,2)|STIRRING TANK(4,2)|ADSORB PHOSPHORUS(4,1)|COAL LIQUEFACTION OIL(4,1)|HYDROCRACKING CATALYST SEM IMAGE(4,1)|MOLYBDENUM ADSORPTION(4,1)|MOTHER LIQUOR(4,1)|RECOVERING MOLYBDENUM(4,1)|SPENT SUPPORTED HYDROGENATION CATALYST(4,1)|SWINGING GLUE FORMING(4,1)|REACTION TEMPERATURE(3,5)|AMMONIA WATER(3,3)|EXTRACTION TIME(3,2)|RAW MATERIAL(3,2)|ALKALINE GLUE FORMING(3,1)|GLUE PH(3,1)|HYDROCRACKING TREATMENT(3,1)|HYDROREFINING OIL NITROGEN CONTENT(3,1)|ION EXCHANGE DEPHOSPHORIZATION(3,1)|PETROLEUM FRACTION(3,1)|VIB CONTENT(3,1)|AFTER ACID TREATMENT(2,4)|ACID GLUE FORMING(2,1)|ADOPTING PH(2,1)|ALKALINE GEL(2,1)|ANNUAL RAPID(2,1)|CALCINATION(2,1)|HYDROCRACKING PERFORMANCE(2,1)|IMPREGNATION LIQUID(2,1)|LEACHING MODE(2,1)|LEACHING SOLUTION(2,1)|MOLYBDENUM SEPARATION(2,1)|NEUTRALIZATION MODE(2,1)|OIL REMOVAL FURNACE(2,1)|PULVERIZATION(2,1)||(CN116440942)|HYDROCRACKING CATALYST(100,38)|RECYCLED WASTE CATALYST(100,1)|SPENT CATALYST(100,1)|WASTE SUPPORTED HYDROCRACKING CATALYST(64,29)|CATALYST RESIDUE(59,10)|ALKALINE SOLUTION(49,14)|CATALYST CARRIER(45,15)|ACIDIC SOLUTION(45,14)|SPENT SUPPORTED HYDROCRACKING CATALYST(33,1)|POWDER GRANULARITY(31,1)|SWINGING GLUE(31,1)|REACTION KETTLE(30,17)|Y MOLECULAR SIEVE(29,21)|ALKALI TREATMENT(29,4)|ORGANIC SOLVENT(28,8)|DEGREASING(28,3)|DECARBONIZATION(28,2)|MOLECULAR SIEVE(27,43)|AQUEOUS SOLUTION(27,10)|ALKALINE GLUE(27,1)|SOLID RESIDUE(26,24)|MOLYBDENUM(24,25)|CRUSHING(24,11)|GLUE PH(23,2)|SIEVING(22,5)|CRACKING PERFORMANCE(22,1)|ALKANE(21,4)|SODIUM METAALUMINATE SOLUTION(20,28)|ACID TREATMENT(20,4)|ORGANIC ALCOHOL(20,4)|PORE VOLUME(20,4)|HYDROTREATMENT(20,1)|CATALYST PARTICLE(19,2)|DEOILING(18,1)|MASS CONTENT(17,12)|PETROLEUM ETHER(17,5)|ACIDIC COMPOUND(17,2)|TRIMETHYLOLETHANE(16,2)|ORGANIC MONOHYDRIC ALCOHOL(15,2)|AGING CONDITION(14,2)|ORGANIC POLYHYDRIC ALCOHOL(14,2)|PENTAERYTHRITOL(14,2)|PORE DIAMETER(14,2)|SWINGING TEMPERATURE(14,2)|STIRRING SPEED(14,1)|ALUMINUM SILICON SOLID RESIDUE(13,3)|MOLAR RATIO(13,2)|ACTIVE METAL COMPONENT(12,3)|DODECANE(12,3)|ALKENE(12,2)|AROMATIC CARBOXYLIC ACID(12,2)|EXTRACTION TEMPERATURE(12,2)|OLEFIN(12,2)|XYLITOL(12,2)|SILICON ALUMINUM MATERIAL(11,28)|AUTOCLAVE(11,15)|ALKALI TREATMENT CONDITION(11,2)|HEXENE(11,2)|PENTANE(11,2)|PENTENE(11,2)|REMOVING OIL(11,2)|SORBITOL(11,2)|PH VALUE(10,17)|NIO WEIGHT CONTENT(10,12)|AGING PH(10,7)|REMOVING CARBON(10,3)|AMMONIUM BICARBONATE(10,2)|GLYCEROL(10,2)|SIO(10,1)|ALUMINUM SULFATE SOLUTION(9,21)|WASHING SOLUTION(9,11)|ACID SALT SOLUTION(9,2)|MOLYBDENUM OXIDE WEIGHT CONTENT(9,2)|SULFUROUS ACID(9,2)|TREATMENT TEMPERATURE(9,2)|UREA(9,2)|RAW MATERIAL ADAPTABILITY(9,1)|REACTION PRESSURE(8,13)|HEATING RATE(8,8)|HEXANE(8,4)|CRYSTAL NUCLEUS(8,3)|ACID TREATMENT CONDITION(8,2)|CARBONIC ACID(8,2)|EXTENSIVE UTILIZATION(8,2)|STOPPING(7,14)|AGING TEMPERATURE(7,7)|CARBON CONTENT(7,6)|ORGANIC ACID(7,4)|EXTRACTING TOLUENE(7,2)|HYDROCRACKING CATALYST CARRIER SUPPORT(7,2)|NICKEL OXIDE WEIGHT CONTENT(7,2)|WASTE SUPPORTED HYDROGENATION CATALYST(7,2)|BASIC SALT SOLUTION(7,1)|HYDROGENATION SPENT CATALYST(7,1)|ISOVOLUMETRIC IMPREGNATION(7,1)|RECOVERED WASTE HYDROCRACKING CATALYST(7,1)|VANADIUM PRECIPITATION TANK(7,1)|WASTE CATALYST COMPREHENSIVE UTILIZATION(7,1)|HEAVY INFERIOR RAW MATERIAL(6,3)|OSCILLATION TIME(6,1)|WASTE HYDROGENATION CATALYST(6,1)|NICKEL SILICON ALUMINUM(5,6)|ACTIVITY EVALUATION(5,2)|ALUMINUM OXIDE(5,2)|AMMONIA WATER(5,2)|CATALYST ACTIVITY(5,2)|GLUE TIME(5,2)|N HEPTANOL(5,2)|N HEXANOL(5,2)|STIRRING TANK(5,2)|ADSORB PHOSPHORUS(5,1)|COAL LIQUEFACTION OIL(5,1)|HYDROCRACKING CATALYST SEM IMAGE(5,1)|MOLYBDENUM ADSORPTION(5,1)|MOTHER LIQUOR(5,1)|RECOVERING MOLYBDENUM(5,1)|SPENT SUPPORTED HYDROGENATION CATALYST(5,1)|SWINGING GLUE FORMING(5,1)|MOO(4,6)|SCREENING(4,6)|REACTION TEMPERATURE(4,5)|AFTER ALKALI TREATMENT(4,3)|EXTRACTION TIME(4,2)|PORE SIZE SURFACE(4,2)|RAW MATERIAL(4,2)|ALKALINE GLUE FORMING(4,1)|HYDROCRACKING TREATMENT(4,1)|HYDROREFINING OIL NITROGEN CONTENT(4,1)|ION EXCHANGE DEPHOSPHORIZATION(4,1)|PETROLEUM FRACTION(4,1)|VIB CONTENT(4,1)|TREATMENT TIME(3,4)|ACID GLUE FORMING(3,1)|ADOPTING PH(3,1)|ALKALINE GEL(3,1)|ANNUAL RAPID(3,1)|CALCINATION(3,1)|HYDROCRACKING PERFORMANCE(3,1)|IMPREGNATION LIQUID(3,1)|LEACHING MODE(3,1)|LEACHING SOLUTION(3,1)|MOLYBDENUM SEPARATION(3,1)|NEUTRALIZATION MODE(3,1)|OIL REMOVAL FURNACE(3,1)|PULVERIZATION(3,1)|REACTION KETTLE VOLUME(3,1)|VIII CONTENT(3,1)|WASHING TANK(3,1)| (CN116440942)|1. A method for recycling a spent catalyst, the method comprising:| (1) Degreasing and decarbonizing the waste supported hydrocracking catalyst, and then crushing and sieving; | (2) Performing alkali treatment on the powder sieved in the step (1) by adopting an alkaline solution to obtain a molybdenum-containing aqueous solution and nickel-containing aluminum-silicon solid residues; | (3) Acid treatment is carried out on the solid residues containing nickel, aluminum and silicon obtained in the step (2) by adopting an acid solution, so as to obtain a nickel-containing aqueous solution and a silicon-aluminum material containing a Y-type molecular sieve; | (4) Adding an organic solvent and the silicon-aluminum material containing the Y molecular sieve obtained in the step (3) into a reaction kettle, stirring, adding an aluminum-containing acidic solution and an aluminum-containing alkaline solution, regulating the pH value to perform a first gel forming reaction, then sequentially and alternately adding the aluminum-containing acidic solution and the aluminum-containing alkaline solution, oscillating to form gel, and aging to obtain a catalyst carrier; | (5) Impregnating the catalyst carrier obtained in the step (4) by using a solution containing an active metal component, and drying and roasting to obtain a novel hydrocracking catalyst; | In the step (1), the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve. |2. The method of claim 1, wherein in step (1), the active metal supported by the spent supported hydrocracking catalyst comprises molybdenum and nickel; the mass content of Al 2O3 -95% and the mass content of Y-type molecular sieve 5-95% based on the mass of the carrier of the waste supported hydrocracking catalyst.|3. The method according to claim 1, wherein in the step (1), the oil removal is performed by a extraction method, the organic solvent used for the extraction is at least one of toluene, petroleum ether and ethanol, the extraction temperature is 80-110 ℃, and the extraction time is 5-60 h.|4. The method according to claim 1, wherein in the step (1), the carbon removal is performed by roasting at a temperature of 500-700 ℃ for 2-48 hours.|5. The method according to claim 1,3 or 4, wherein in the step (1), the weight content of nickel oxide in the waste supported hydrocracking catalyst after degreasing and decarbonizing is 2-10%, the weight content of molybdenum oxide is 15-50%, and the weight content of carbon is less than 1%; the granularity of the powder obtained after crushing and sieving is 200-400 meshes.|6. The method according to claim 1, wherein in the step (2), the alkaline solution is one or more of ammonia water, urea, ammonium carbonate and ammonium bicarbonate, and the concentration is 5g/100mL to 100g/100mL; the liquid-solid mass ratio of the alkaline solution to the powder sieved in the step (1) is 1:1 to 50:1.|7. The method according to claim 6, wherein in the step (2), the concentration of the alkaline solution is 10g/100 mL-90 g/100mL; the liquid-solid mass ratio of the alkaline solution to the powder sieved in the step (1) is 2:1 to 45:1.|8. The method according to claim 1, wherein in step (2), the alkali treatment conditions are as follows: the temperature is 100-400 ℃, the treatment time is 0.5-4.0 h, the pressure is 5-20 MPa, and the rate of heating to the treatment temperature is 5-25 ℃/min; after alkali treatment, the leaching rate of the molybdenum oxide is 90% -98%.|9. The method according to claim 8, wherein in step (2), the alkali treatment is performed under the following conditions: the temperature is 150-350 ℃, the treatment time is 0.5-3.0 h, the pressure is 5-15 MPa, and the rate of heating to the treatment temperature is 5-10 ℃/min; after alkali treatment, the leaching rate of the molybdenum oxide is 95-98 percent.|10. The method according to claim 1, wherein in the step (3), the acidic solution is one or more of oxalic acid, carbonic acid, EDTA, acetic acid and sulfurous acid, and the concentration thereof is 5g/100 mL-100 g/100mL; the liquid-solid mass ratio of the acidic compound in the acidic solution to the solid residue containing nickel-silicon-aluminum obtained in the step (2) is 1:1 to 50:1.|11. The method of claim 10, wherein in step (3), the concentration of the acidic solution is 10g/100mL to 90g/100mL; the liquid-solid mass ratio of the acidic compound in the acidic solution to the solid residue containing nickel-silicon-aluminum obtained in the step (2) is 2:1 to 45:1.|12. The method according to claim 1, wherein in step (3), the acid treatment conditions are as follows: the temperature is 100-400 ℃, the treatment time is 0.5-4.0 h, the reaction pressure is 5-20 MPa, and the heating rate is 5-25 ℃/min; after acid treatment, the leaching rate of nickel oxide is 90% -98%.|13. The method of claim 12, wherein in step (3), the acid treatment conditions are as follows: the temperature is 150-350 ℃, the treatment time is 0.5-3.0 h, the reaction pressure is 5-15 MPa, and the heating rate is 5-10 ℃/min; after acid treatment, the leaching rate of the nickel oxide is 95-98%.|14. The method of claim 1, wherein in step (3), the molar ratio of SiO 2/Al2O3 of the Y molecular sieve-containing aluminosilicate material is 2:1 to 50:1, the pore volume is 0.4-0.8 mL.g -1; the specific surface area is 650-750 m 2·g-1; the pore size can be less than 5nm.|15. The method of claim 14, wherein in step (3), the molar ratio of SiO 2/Al2O3 of the Y molecular sieve-containing aluminosilicate material is 2:1 to 25:1, the pore diameter is 5-7 nm.|16. The method of claim 1, wherein in step (4), the organic solvent is one or more of an alkane, an alkene, an organic alcohol, and an organic acid.|17. The method of claim 16, wherein the alkane is at least one of pentane, hexane, dodecane; the olefin is at least one of pentene and hexene; the organic alcohol is selected from at least one of organic monohydric alcohol and organic polyhydric alcohol; the organic acid is at least one selected from aliphatic or aromatic carboxylic acids.|18. The method of claim 17, wherein the organic alcohol is at least one of n-hexanol, n-heptanol, pentaerythritol, glycerol, trimethylolethane, xylitol, sorbitol.|19. The method according to claim 1, wherein in the step (4), the concentration of the aluminum-containing alkaline solution is 10 to 20g/100mL in terms of alumina; the concentration of the aluminum-containing acidic solution is 5-10 g/100mL calculated by alumina.|20. The method of claim 1, wherein in step (4), the first glue has a pH of 7.0 to 9.0 for 3 to 15 minutes at 50 to 100 ℃; and/or the number of the groups of groups,|The time of each glue forming in the swinging glue forming is 3-15 min, the temperature of the swinging glue forming is 50-100 ℃, the pH value of the swinging glue forming is adjusted to be 2.0-3.0 in the acid glue forming process, the pH value of the swinging glue forming process is adjusted to be 10.0-11.0 in the alkaline glue forming process, the swinging times are 2-8 times, the whole glue forming process is carried out under stirring, and the stirring speed is 20-500 rad/min.|21. The method of claim 20, wherein in step (4), the temperature of the first glue is 70 to 100 ℃.|22. The method of claim 1, wherein in step (4), the aging conditions are as follows: the pH value is 7.0-9.0, the temperature is 50-100 ℃ and the time is 0.5-2.5 h.|23. The method of claim 22, wherein in step (4), the aging conditions are as follows: the temperature is 70-100 ℃ and the time is 1.0-2.0 h.|24. A novel hydrocracking catalyst prepared by the process according to any one of claims 1 to 23, characterized in that: the content of the carrier is 65-95% by weight of the catalyst, and the content of the active metal is 5-35% by weight of the oxide; with R as the radius of the catalyst particles, the silicon-aluminum material containing the Y-type molecular sieve is distributed in the range from the center to R/2-2R/3, and the aluminum oxide is distributed in the range from R/2-2R/3 to R.|25. The novel hydrocracking catalyst of claim 24, wherein the novel hydrocracking catalyst has the following properties: the pore volume is 1.5-2.0 mL.g -1; the specific surface area is 300-450 m 2·g-1; the pore diameter is not less than 10nm; the particle size distribution is as follows: the proportion of the particle size less than 100 mu m is 0.5% -1%, the proportion of the particle size of 100-200 mu m is 2% -5%, and the proportion of the particle size more than 200 mu m is 90% -95%.|26. The novel hydrocracking catalyst of claim 24, wherein the novel hydrocracking catalyst has a cocoa aperture of from 15 to 25nm.|27. Use of a novel hydrocracking catalyst according to claim 24 or 25 or 26, characterized in that: the novel hydrocracking catalyst is applied to the hydrotreatment of heavy inferior raw materials. (CN116440942)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to a method for recycling a waste catalyst, in particular to a method for recycling a waste supported hydrocracking catalyst to prepare a novel hydrocracking catalyst.|BACKGROUND ART|[0002] The primary treatment of spent supported hydrogenation catalysts in the past has been landfills. However, the current production of waste supported hydrogenation catalysts in China exceeds 100000 tons each year, and the annual rapid increase of the catalyst still occurs at a rate of 4.4%, so that development of efficient technology for efficiently treating and cleaning and recycling toxic metal pollutants in the waste supported hydrogenation catalysts is needed.|[0003] CN107723468a discloses a comprehensive utilization system of waste catalyst. The system comprises an oil removal furnace, a rotary kiln, a four-stage countercurrent device, a stirring tank I, a plate and frame filter I, a precipitation tank I, a plate and frame filter II, a stirring tank II, a centrifugal machine I, ion exchange resin, an extraction device, a back extraction device, a precipitation tank II, a centrifugal machine II and a washing tank. The process can effectively recycle the useful components in the residual oil hydrogenation spent catalyst to obtain products such as industrial steam, nickel aluminum powder, ammonium metavanadate, high-purity molybdic acid, anhydrous sodium sulfate, distilled water and the like, and can obtain the high-purity molybdic acid without multiple separation processes, but the process is complex.|[0004] CN104628032B discloses a method for preparing high-purity ammonium metavanadate from waste catalyst. The method comprises the following steps: collecting the waste catalyst leaching solution by utilizing a leaching mode, filtering the leaching solution, then entering an ion exchange dephosphorization system, and utilizing resin to adsorb phosphorus and adsorb the phosphorus in the waste catalyst leaching solution; after dephosphorization, the molybdenum-vanadium-containing solution enters an ion exchange system, and molybdenum adsorption is carried out by using resin, so that molybdenum and vanadium are separated; pumping the vanadium-containing mother liquor after dephosphorization and molybdenum separation into a vanadium precipitation tank, and carrying out weak alkaline ammonium salt vanadium precipitation to obtain a high-purity ammonium metavanadate product. The method has the characteristics of short flow, simple process, energy conservation, environmental protection, high efficiency, low cost and the like, but can not make full use of things and can not fully mine the value of the waste hydrogenation catalyst.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the defects of the prior art, the invention provides a method for recycling a waste catalyst, which takes the waste supported hydrocracking catalyst as a raw material to prepare a novel hydrocracking catalyst, the method has the characteristics of simple preparation process, high metal recovery rate, low treatment cost and the like, and the obtained hydrocracking catalyst has good hydrogenation and cracking performances and better raw material adaptability.|[0006] The invention provides a method for recycling a waste catalyst, which comprises the following steps:|[0007] (1) Degreasing and decarbonizing the waste supported hydrocracking catalyst, and then crushing and sieving; |[0008] (2) Performing alkali treatment on the powder sieved in the step (1) by adopting an alkaline solution to obtain a molybdenum-containing aqueous solution and nickel-containing aluminum-silicon solid residues; |[0009] (3) Acid treatment is carried out on the solid residues containing nickel, aluminum and silicon obtained in the step (2) by adopting an acid solution, so as to obtain a nickel-containing aqueous solution and a silicon-aluminum material containing a Y-type molecular sieve; |[0010] (4) Adding an organic solvent and the silicon-aluminum material containing the Y molecular sieve obtained in the step (3) into a reaction kettle, stirring, adding an aluminum-containing acidic solution and an aluminum-containing alkaline solution, regulating the pH value to perform a first gel forming reaction, then sequentially and alternately adding the aluminum-containing acidic solution and the aluminum-containing alkaline solution, oscillating to form gel, and aging to obtain a catalyst carrier; |[0011] (5) And (3) impregnating the catalyst carrier obtained in the step (4) by using a solution containing an active metal component, and drying and roasting to obtain the novel hydrocracking catalyst. |[0012] In the method of the invention, in the step (1), the content of catalyst solids is 70-90% and the content of petroleum fraction is 10-30% by weight of the waste supported hydrocracking catalyst.|[0013] In the method of the present invention, in the step (1), the active metal supported by the waste supported hydrocracking catalyst includes molybdenum and nickel. The waste supported hydrocracking catalyst carrier comprises Al 2O3 -95% of Al 2O3 and 5-95% of Y-type molecular sieve by weight of the carrier.|[0014] In the method of the present invention, in the step (1), the oil removal is generally performed by a extraction method. The organic solvent adopted in the extraction is at least one of toluene, petroleum ether, ethanol and the like, the extraction temperature is 80-110 ℃, and the extraction time is 5-60 h.|[0015] In the method of the present invention, in the step (1), the carbon removal may be performed by a calcination method, wherein the calcination temperature is 500-700 ℃, preferably 600-650 ℃, and the calcination time is 2-48 hours, preferably 5-24 hours. The weight content of nickel oxide in the waste supported hydrocracking catalyst after oil removal and carbon removal is 2% -10%, the weight content of molybdenum oxide is 15% -50%, and the weight content of carbon is less than 1%.|[0016] In the process of the present invention, in the step (1), the particle size of the powder obtained after the pulverization and sieving is 200 to 400 mesh, preferably 300 to 400 mesh.|[0017] In the method of the invention, in the step (2), the alkaline solution is one or more of ammonia water, urea, ammonium carbonate, ammonium bicarbonate and the like, and the concentration of the alkaline solution is 5g/100 mL-100 g/100mL, preferably 10g/100 mL-90 g/100mL; the liquid-solid mass ratio of the alkaline solution to the powder sieved in the step (1) is 1:1 to 50:1, preferably 2:1 to 45:1.|[0018] In the method of the present invention, in the step (2), the conditions of the alkali treatment are as follows: the temperature is 100-400 ℃, preferably 150-350 ℃, the treatment time is 0.5-4.0 h, preferably 0.5-3.0 h, the pressure is 5-20 MPa, preferably 5-15 MPa, and the rate of heating to the treatment temperature is 5-25 ℃/min, preferably 5-10 ℃/min.|[0019] In the method, in the step (2), after alkali treatment, conventional filtration, washing and drying are carried out to obtain the molybdenum-containing water solution and the nickel-containing aluminum-silicon solid residue. Preferably, the leaching rate of the molybdenum oxide is 90-98%, preferably 95-98% after alkali treatment. The leaching rate of molybdenum oxide is the ratio of the mass of molybdenum in the molybdenum-containing aqueous solution to the mass of molybdenum in the waste supported hydrocracking catalyst, calculated as molybdenum oxide.|[0020] In the method of the present invention, in the step (3), the acidic solution is one or more of oxalic acid, carbonic acid, EDTA, acetic acid, sulfurous acid, etc., and the concentration thereof is 5g/100 mL-100 g/100mL, preferably 10g/100 mL-90 g/100mL. The liquid-solid mass ratio of the acidic compound in the acidic solution to the solid residue containing nickel-silicon-aluminum obtained in the step (2) is 1:1 to 50: 1, preferably 2:1 to 45:1.|[0021] In the method of the present invention, in the step (3), the conditions of the acid treatment are as follows: the temperature is 100-400 ℃, preferably 150-350 ℃, the treatment time is 0.5-4.0 h, preferably 0.5-3.0 h, the reaction pressure is 5-20 MPa, preferably 5-15 MPa, and the heating rate is 5-25 ℃/min, preferably 5-10 ℃/min. Preferably, the leaching rate of nickel oxide after acid treatment is 90% -98%, preferably 95% -98%. The leaching rate of nickel oxide is calculated as nickel oxide, and the ratio of the mass of nickel in the nickel-containing aqueous solution to the mass of nickel in the waste supported hydrocracking catalyst.|[0022] In the method, in the step (3), after acid treatment, the water solution containing nickel and the silicon-aluminum material containing the Y-type molecular sieve are obtained through conventional filtration, washing and drying.|[0023] In the method of the invention, in the step (3), the SiO 2/Al2O3 mol ratio of the silicon aluminum material containing the Y molecular sieve is 2:1 to 50: 1, preferably 2:1 to 25:1, the pore volume is 0.4-0.8 mL.g -1; the specific surface area is 650-750 m 2·g-1; the pore size may be less than 5nm, preferably 5 to 7nm.|[0024] In the method of the present invention, in the step (4), the organic solvent is one or more of alkane, alkene, organic alcohol, organic acid, etc., and further, the alkane is preferably at least one of pentane, hexane, dodecane, etc.; the olefin is preferably at least one of pentene, hexene and the like; the organic alcohol is at least one selected from organic monohydric alcohol and organic polyhydric alcohol, preferably at least one selected from n-hexanol, n-heptanol, pentaerythritol, glycerol, trimethylolethane, xylitol, sorbitol, etc.; the organic acid is at least one selected from aliphatic or aromatic carboxylic acids, such as benzoic acid, etc. The addition amount of the organic solvent is 1/5-1/2 of the actual effective use volume of the reaction kettle.|[0025] In the method of the invention, in the step (4), the concentration of the aluminum-containing alkaline salt solution calculated by alumina is 10-20 g/100mL; the concentration of the aluminum-containing acidic salt solution is 5-10 g/100mL calculated by alumina.|[0026] In the method of the present invention, in the step (4), the pH of the first glue is 7.0-9.0, the time is 3-15 min, and the temperature is 50-100 ℃, preferably 70-100 ℃;|[0027] The time of each glue forming in the swinging glue forming is 3-15 min, and the temperature of the swinging glue forming is 50-100 ℃, preferably 70-100 ℃. The pH value is adjusted to 2.0-3.0 during acid gel forming and 10.0-11.0 during alkaline gel forming, and the oscillating times are 2-8 times, preferably 3-5 times. The entire gelling process is carried out with stirring at a rate of 20 to 500rad/min, preferably 20 to 300rad/min. |[0028] In the method of the present invention, in the step (4), the aging conditions are as follows: the pH value is 7.0-9.0, the temperature is 50-100 ℃, preferably 70-100 ℃, and the time is 0.5-2.5 h, preferably 1.0-2.0 h.|[0029] In the method of the invention, in the step (4), after aging, the catalyst carrier is obtained through conventional filtration, drying and roasting.|[0030] In the process according to the invention, in step (5), the active metal is selected from one or more of the group VIII and/or group VIB metal elements, preferably one or more of tungsten, molybdenum, cobalt or nickel.|[0031] In the method of the present invention, in the step (5), the impregnation liquid containing active metal may be an aqueous solution containing molybdenum recovered in the step (2) or the step (3) or an aqueous solution containing nickel.|[0032] In the process of the present invention, in step (5), the impregnation may be carried out by impregnation means conventional in the art, such as isovolumetric impregnation, etc. The drying temperature is 100-200 ℃, preferably 120-150 ℃, the drying time is 2-10 h, the roasting temperature is 300-800 ℃, preferably 350-550 ℃, and the roasting time is 2.0-5.0 h, preferably 2.0-4.0 h.|[0033] The novel hydrocracking catalyst obtained by the invention takes R as the radius of catalyst particles, the silicon-aluminum material containing the Y-type molecular sieve is distributed in the range from the center to R/2-2R/3, and the aluminum oxide is distributed in the range from R/2-2R/3 to R.|[0034] The novel hydrocracking catalyst provided by the invention has the following properties: the pore volume is 1.5-2.0 mL.g -1; the specific surface area is 300-450 m 2·g-1; the pore diameter is not less than 10nm, preferably 15-25 nm; the particle size distribution is as follows: the proportion of the particle size less than 100 mu m is 0.5% -1%, the proportion of the particle size of 100-200 mu m is 2% -5%, and the proportion of the particle size more than 200 mu m is 90% -95%.|[0035] In the novel hydrocracking catalyst, the carrier content is 65-95% by weight of the catalyst, and the content of active metal calculated by oxide is 5-35%. Further, the content of the VIII group metal in an oxidation state is 3-30% and the content of the VIB group metal in an oxide is 0.5-5% based on the weight of the catalyst.|[0036] The invention also provides an application of the novel hydrocracking catalyst, the application is that the novel hydrocracking catalyst is applied to hydrocracking treatment of heavy inferior raw materials.|[0037] The heavy inferior raw materials comprise at least one of raw materials such as diesel oil, wax oil, residual oil, coal tar, coal liquefied oil and the like.|[0038] Compared with the prior art, the invention has the following advantages:|[0039] the method of the invention firstly carries out acid solution and alkaline solution treatment on the recovered waste hydrocracking catalyst, obtains the silicon-aluminum material which keeps the complete structure of the Y molecular sieve on the basis of recovering molybdenum and nickel solution, takes the material in the specific state as crystal nucleus, firstly mixes the crystal nucleus with organic solvent, forms alumina carrier material on the outer layer of the crystal nucleus by adopting pH swing neutralization mode, and the prepared catalyst has excellent hydrocracking performance and is suitable for processing inferior raw materials. |[0040] The method of the invention realizes the recycling of the waste hydrocracking catalyst, greatly reduces the production cost of the catalyst and improves the comprehensive utilization value of the waste catalyst.|DRAWINGS DESCRIPTION|[0041] FIG. 1 is an SEM image of a novel hydrocracking catalyst A obtained from example 1.|INVENTION MODE|Detailed Description|[0042] The present invention will be further described with reference to examples, but it should be understood that the scope of the present invention is not limited by the examples. In the present invention, percentages and percentages are by mass unless explicitly stated otherwise.|[0043] The SEM image of the invention is measured by a field emission scanning electron microscope (JSM 7500F), and the electron gun type is as follows: cold field emission gun, accelerating voltage: 0.1 kW-30 kW, resolution: 1.0nm (secondary electrons), 3.0nm (backscattered electrons), magnification: 25 to 1000000.|[0044] Example 1|[0045] The method comprises the steps of extracting 30% of oil-containing waste supported hydrocracking catalyst (the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve, the mass content of Al 2O3 is 80% and the mass content of the Y-type molecular sieve is 20%) with petroleum ether at 100 ℃ for 48 hours, roasting at 600 ℃ for 10 hours, wherein the obtained waste supported hydrocracking catalyst has the weight content of MoO 3 of 25.5%, the weight content of NiO of 8.5% and the carbon content of less than or equal to 0.9%, and then obtaining 300-400 mesh powder after crushing and screening.|[0046] Uniformly mixing an ammonium carbonate solution with the concentration of 25g/100mL and 100g of powder according to the liquid-solid mass ratio of 10:1, adding the mixture into an autoclave, heating to 200 ℃ at the heating rate of 5 ℃/min, reacting at the reaction pressure of 10.0MPa for 2.5 hours at the constant temperature, filtering and washing until the washing solution is neutral, and drying at 150 ℃ for 2 hours to obtain a molybdenum-containing solution and a nickel-silicon-aluminum-containing solid residue, wherein the leaching rate of MoO 3 is 98%.|[0047] Oxalic acid solution with the concentration of 20g/100mL and the solid residue containing nickel and silicon aluminum with the concentration of 75g are uniformly mixed according to the mass ratio of 10:1, the mixture is added into an autoclave, the temperature is raised to 250 ℃ at the heating rate of 10 ℃/min, the reaction pressure is 13.0MPa, the constant temperature time is 3 hours, and the mixture is filtered and washed until the washing solution is neutral, and the mixture is dried at 120 ℃ for 4 hours to obtain nickel-containing solution and silicon aluminum material A containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.8%.|[0048] Adding 50g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 5L of normal hexane into the reaction kettle, controlling the stirring speed to be 150rad/min, then adding a sodium metaaluminate solution with the concentration of 15g/100mL at the speed of 5mL/min, simultaneously adding an aluminum sulfate solution with the concentration of 5g/100mL, controlling the pH value to be 7.5, controlling the temperature to be 75 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 5g/100mL, stopping adding when the pH value is controlled to be 3.0, and stabilizing for 5 min; then adding 15g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to 11.0, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to 9.0, controlling the aging temperature to 100 ℃, aging for 2h, filtering, drying at 150 ℃ for 5h, and roasting at 500 ℃ for 4h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried at 120 ℃ for 3 hours and baked at 450 ℃ for 3 hours, so that the novel hydrocracking catalyst A is obtained, and the properties of the novel hydrocracking catalyst A are shown in table 2.|[0049] Example 2|[0050] The method comprises the steps of extracting a waste supported hydrocracking catalyst containing 25% of oil by using a petroleum ether and diethyl ether mixed solution with a volume ratio of 1:1 at 90 ℃ for 50 hours, roasting at 650 ℃ for 5 hours, wherein the waste supported hydrocracking catalyst contains 24.7% of MoO 3, 8.8% of NiO and less than or equal to 0.8% of carbon by weight, and the powder with 300-400 meshes is obtained after crushing and screening, wherein the waste supported hydrocracking catalyst carrier comprises Al 2O3 and Y-type molecular sieves, and the mass content of Al 2O3 is 95% and the mass content of Y-type molecular sieves is 5% based on the mass of the carrier.|[0051] Mixing 30g/100mL ammonia water solution and 250g of the powder according to a liquid-solid mass ratio of 15:1, uniformly adding the mixture into an autoclave, heating to 280 ℃ at a heating rate of 10 ℃/min, reacting at a reaction pressure of 13.0MPa for 3.0h, filtering and washing until a washing solution is neutral, and drying at 140 ℃ for 4h to obtain a molybdenum-containing solution and a nickel-silicon-containing solid residue, wherein the leaching rate of MoO 3 is 97%.|[0052] Uniformly mixing 15g/100mL of EDTA solution and 186g of nickel-containing silicon-aluminum solid residues according to a liquid-solid mass ratio of 18:1, adding the mixture into an autoclave, heating to 200 ℃ at a heating rate of 10 ℃/min, reacting at 15.0MPa for 2.5 hours at a constant temperature, filtering and washing until a washing solution is neutral, and drying at 150 ℃ for 3 hours to obtain a nickel-containing solution and a silicon-aluminum material B containing a Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 98%.|[0053] Crushing 100g of silicon-aluminum material containing the Y molecular sieve, adding 10L of n-hexylene alcohol into a reaction kettle, controlling the stirring speed to be 200rad/min, adding 12g/100mL of sodium metaaluminate solution at the speed of 10mL/min, simultaneously adding 10g/100mL of aluminum sulfate solution, controlling the pH value to be 8.5, controlling the temperature to be 90 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 10g/100mL, stopping adding when the pH value is controlled to be 2.0, and stabilizing for 5 min; then adding 12g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to be 10.0, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to 8.5, controlling the aging temperature to 100 ℃, aging for 1.5h, filtering, drying at 200 ℃ for 2h, and roasting at 500 ℃ for 4h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried at 150 ℃ for 2 hours and baked at 550 ℃ for 4 hours, so that the novel hydrocracking catalyst B is obtained, and the properties of the novel hydrocracking catalyst B are shown in table 2.|[0054] Example 3|[0055] The method comprises the steps of extracting a waste supported hydrocracking catalyst containing 28% of oil (the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve, the mass content of the Al 2O3 is 70% and the mass content of the Y-type molecular sieve is 30% based on the mass of the carrier) with toluene at 110 ℃ for 32 hours, roasting the waste supported hydrocracking catalyst at 630 ℃ for 12 hours, wherein the obtained waste supported hydrocracking catalyst has the MoO 3 weight content of 26.9%, the NiO weight content of 9.6% and the carbon content of less than or equal to 1.0%, and then obtaining 300-400 mesh powder after crushing and screening.|[0056] Uniformly mixing urea solution with the concentration of 45g/100mL and the 500g powder according to the mass ratio of liquid to solid of 20:1, adding the mixture into an autoclave, heating the autoclave to 300 ℃ at the heating rate of 8 ℃/min, reacting the mixture under the pressure of 15.0MPa, keeping the temperature for 2.0h, filtering and washing the mixture until the washing solution is neutral, and drying the mixture at 140 ℃ for 4h to obtain molybdenum-containing solution and nickel-silicon-containing solid residues, wherein the leaching rate of MoO 3 is 97.9%.|[0057] Acetic acid solution with the concentration of 30g/100mL and 379g of solid residue containing nickel-silicon-aluminum are evenly mixed according to the mass ratio of liquid to solid of 20:1, the mixture is added into an autoclave, the temperature is raised to 270 ℃ at the heating rate of 10 ℃/min, the reaction pressure is 14.6MPa, the constant temperature time is 2.0h, and the mixture is filtered and washed until washing liquid is neutral, and the mixture is dried at 150 ℃ for 5h to obtain nickel-containing solution and silicon-aluminum material C containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.9%.|[0058] Adding 300g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 20L of styrene into the reaction kettle, controlling the stirring speed to be 190rad/min, then adding 20g/100mL of sodium metaaluminate solution at a speed of 25mL/min, simultaneously adding 8g/100mL of aluminum sulfate solution, controlling the pH value to be 8.0, controlling the reaction temperature to be 95 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 8g/100mL, stopping adding when the pH value is controlled to be 2.0, and stabilizing for 5 min; then adding 20g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to be 10.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to be 7.5, controlling the aging temperature to be 95 ℃, aging for 2.0h, filtering, drying at 150 ℃ for 3h, and roasting at 550 ℃ for 5h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried for 5 hours at 140 ℃ and baked for 3 hours at 400 ℃, so that the novel hydrocracking catalyst C is obtained, and the properties of the novel hydrocracking catalyst C are shown in Table 2.|[0059] Example 4|[0060] The method comprises the steps of (1) adopting a volume ratio of a waste supported hydrocracking catalyst containing 20% of oil (the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve, wherein the mass content of Al 2O3 is 45% and the mass content of the Y-type molecular sieve is 55%) based on the mass of the carrier: 1, extracting toluene and petroleum ether at 110 ℃ for 36 hours, roasting at 650 ℃ for 8 hours, wherein the weight content of MoO 3 and the weight content of NiO are respectively 27.5% and less than or equal to 0.8%, and then crushing and screening to obtain 300-400 mesh powder.|[0061] Uniformly mixing 20g/100mL of ammonium carbonate solution and 200g of powder according to a liquid-solid mass ratio of 8:1, adding the mixture into an autoclave, heating to 220 ℃ at a heating rate of 10 ℃/min, reacting at a reaction pressure of 11.0MPa for 2.0h, filtering and washing until a washing solution is neutral, and drying at 150 ℃ for 3h to obtain a molybdenum-containing solution and a nickel-silicon-containing solid residue, wherein the leaching rate of MoO 3 is 98%.|[0062] Oxalic acid solution with the concentration of 25g/100mL and 175g of solid residues containing nickel and silicon aluminum are uniformly mixed according to the mass ratio of liquid to solid of 8:1, the mixture is added into an autoclave, the temperature is raised to 300 ℃ at the heating rate of 8 ℃/min, the reaction pressure is 15.0MPa, the constant temperature time is 2.5h, and the mixture is filtered and washed until the washing solution is neutral, and the mixture is dried at 180 ℃ for 2h to obtain nickel-containing solution and silicon aluminum material D containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.5%.|[0063] Adding 150g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 10L of hexane into the reaction kettle, controlling the stirring speed to be 150rad/min, then adding a sodium metaaluminate solution with the concentration of 20g/100mL at the speed of 10mL/min, simultaneously adding an aluminum sulfate solution with the concentration of 10g/100mL, controlling the pH value to be 7.0, controlling the reaction temperature to be 85 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 10g/100mL, stopping adding when the pH value is controlled to be 3.2, and stabilizing for 5 min; then adding 20g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to 11.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 4 times, adjusting the aging pH value to 9.0, controlling the aging temperature to 90 ℃, aging for 3h, filtering, drying at 120 ℃ for 5h, and baking at 500 ℃ for 3h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried for 3 hours at 120 ℃ and baked for 3 hours at 450 ℃ to obtain the novel hydrocracking catalyst D, wherein the properties of the novel hydrocracking catalyst D are shown in table 2.|[0064] Example 5|[0065] The method comprises the steps of (1) adopting a volume ratio of a waste supported hydrocracking catalyst containing 25% of oil (the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve, wherein the mass content of Al 2O3 is 60% and the mass content of the Y-type molecular sieve is 40%) based on the mass of the carrier: 1, extracting toluene and diethyl ether at 110 ℃ for 38 hours, roasting at 620 ℃ for 8 hours, wherein the weight content of MoO 3 and the weight content of NiO are respectively 26.5% and 8.9% and less than or equal to 0.9%, and crushing and screening to obtain 300-400 mesh powder.|[0066] Uniformly mixing 40g/100mL ammonium carbonate solution and 300g of powder according to a liquid-solid mass ratio of 5:1, adding the mixture into an autoclave, heating to 250 ℃ at a heating rate of 10 ℃/min, reacting at a reaction pressure of 13.0MPa for 2.0h, filtering and washing until a washing solution is neutral, and drying at 130 ℃ for 4h to obtain a molybdenum-containing solution and a nickel-silicon-containing solid residue, wherein the leaching rate of MoO 3 is 97.5%.|[0067] Oxalic acid solution with the concentration of 15g/100mL and the solid residue containing nickel and silicon aluminum with the concentration of 269g are uniformly mixed according to the mass ratio of liquid to solid of 20:1, the mixture is added into an autoclave, the temperature is raised to 300 ℃ at the heating rate of 8 ℃/min, the reaction pressure is 15.0MPa, the constant temperature time is 2.5h, the mixture is filtered and washed until the washing solution is neutral, and the mixture is dried at 150 ℃ for 5h, so that nickel-containing solution and silicon aluminum material E containing Y molecular sieve are obtained, the properties of the nickel-containing solution and the silicon aluminum material E are shown in Table 1, and the leaching rate of NiO is 98.0%.|[0068] Adding 100g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 15L of dodecane into the reaction kettle, controlling the stirring speed to be 120rad/min, then adding a sodium metaaluminate solution with the concentration of 16g/100mL at the speed of 6mL/min, simultaneously adding an aluminum sulfate solution with the concentration of 15g/100mL, controlling the pH value to be 7.0, controlling the reaction temperature to be 85 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding an aluminum sulfate solution with the concentration of 15g/100mL, stopping adding when the pH value is controlled to be 3.0, and stabilizing for 5 min; then adding 16g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to 11.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to 10.0, controlling the aging temperature to 95 ℃, aging for 3.0h, filtering, drying at 170 ℃ for 2h, and roasting at 450 ℃ for 4h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried for 3 hours at 120 ℃ and baked for 3 hours at 450 ℃ to obtain the novel hydrocracking catalyst E, wherein the properties of the novel hydrocracking catalyst E are shown in table 2.|[0069] Comparative example 1|[0070] Adding an outsourced 350g Y molecular sieve (the properties of which are shown in table 1) into a reaction kettle, adding 15L of purified water into the reaction kettle, controlling the stirring speed to 190rad/min, controlling the reaction temperature to 95 ℃, then controlling the adding speed of a sodium metaaluminate solution with the concentration of 20g/100mL to 25mL/min, simultaneously adding an aluminum sulfate solution with the concentration of 8g/100mL, controlling the pH value to 8.0, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 8g/100mL, stopping adding when the pH value is controlled to be 2.0, and stabilizing for 5 min; then adding 20g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to be 10.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, adjusting the aging pH value to be 7.5 after swinging for 3 times, controlling the aging temperature to be 95 ℃, aging for 2.0h, filtering, drying at 150 ℃ for 3h, and roasting at 550 ℃ for 3h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried at 140 ℃ for 5 hours and baked at 400 ℃ for 3 hours, so that the hydrocracking catalyst F is obtained, and the properties of the hydrocracking catalyst F are shown in table 2.|[0071] Comparative example 2|[0072] The waste supported hydrocracking catalyst (same as in example 3) containing 28% of oil is extracted by toluene at 110 ℃ for 32 hours, and then baked at 630 ℃ for 12 hours, the weight content of MoO 3 of the obtained waste supported hydrocracking catalyst is 26.9%, the weight content of NiO is 9.6%, the carbon content is less than or equal to 1.0%, and then crushed and sieved to obtain 300-400 mesh powder.|[0073] Uniformly mixing urea solution with the concentration of 45g/100mL and the 500g powder according to the mass ratio of liquid to solid of 20:1, adding the mixture into an autoclave, heating the autoclave to 300 ℃ at the heating rate of 8 ℃/min, reacting the mixture under the pressure of 15.0MPa, keeping the temperature for 2.0h, filtering and washing the mixture until the washing solution is neutral, and drying the mixture at 140 ℃ for 4h to obtain molybdenum-containing solution and nickel-silicon-containing solid residues, wherein the leaching rate of MoO 3 is 97.9%.|[0074] Acetic acid solution with the concentration of 30g/100mL and 379g of solid residue containing nickel-silicon-aluminum are evenly mixed according to the mass ratio of liquid to solid of 20:1, the mixture is added into an autoclave, the temperature is raised to 270 ℃ at the heating rate of 10 ℃/min, the reaction pressure is 14.6MPa, the constant temperature time is 2.0h, and the mixture is filtered and washed until washing liquid is neutral, and the mixture is dried at 150 ℃ for 5h to obtain nickel-containing solution and silicon-aluminum material C containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.9%.|[0075] The molybdenum-containing solution and the nickel-containing solution are immersed to obtain a silicon-aluminum material G containing the Y molecular sieve, the silicon-aluminum material G is dried for 5 hours at 140 ℃ and baked for 3 hours at 400 ℃, and the hydrocracking catalyst G is obtained, and the properties of the hydrocracking catalyst G are shown in Table 2.|[0076] Comparative example 3|[0077] The waste supported hydrocracking catalyst (same as in example 3) containing 28% of oil is extracted by toluene at 110 ℃ for 32 hours, and then baked at 630 ℃ for 12 hours, the weight content of MoO 3 of the obtained waste supported hydrocracking catalyst is 26.9%, the weight content of NiO is 9.6%, the carbon content is less than or equal to 1.0%, and then crushed and sieved to obtain 300-400 mesh powder.|[0078] Uniformly mixing urea solution with the concentration of 45g/100mL and the 500g powder according to the mass ratio of liquid to solid of 20:1, adding the mixture into an autoclave, heating the autoclave to 300 ℃ at the heating rate of 8 ℃/min, reacting the mixture under the pressure of 15.0MPa, keeping the temperature for 2.0h, filtering and washing the mixture until the washing solution is neutral, and drying the mixture at 140 ℃ for 4h to obtain molybdenum-containing solution and nickel-silicon-containing solid residues, wherein the leaching rate of MoO 3 is 97.9%.|[0079] Acetic acid solution with the concentration of 30g/100mL and 379g of solid residue containing nickel-silicon-aluminum are evenly mixed according to the mass ratio of liquid to solid of 20:1, the mixture is added into an autoclave, the temperature is raised to 270 ℃ at the heating rate of 10 ℃/min, the reaction pressure is 14.6MPa, the constant temperature time is 2.0H, and the mixture is filtered and washed until washing liquid is neutral, and the mixture is dried at 150 ℃ for 5H to obtain nickel-containing solution and silicon-aluminum material H containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.9%.|[0080] Adding 300g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 20L of purified water into the reaction kettle, controlling the stirring speed to be 190rad/min, adding 20g/100mL of sodium metaaluminate solution at the speed of 25mL/min, simultaneously adding 8g/100mL of aluminum sulfate solution, controlling the pH value to be 8.0, controlling the reaction temperature to be 95 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuing to add the aluminum sulfate solution with the concentration of 8g/100mL, stopping adding when the pH value is controlled to be 2.0, and stabilizing for 5 min; then adding 20g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to be 10.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to be 7.5, controlling the aging temperature to be 95 ℃, aging for 2.0h, filtering, drying at 150 ℃ for 3h, and roasting at 550 ℃ for 5h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried at 140 ℃ for 5 hours and baked at 400 ℃ for 3 hours, so that the hydrocracking catalyst H is obtained, and the properties of the hydrocracking catalyst H are shown in table 2.|[0081] TABLE 1|[0082] |[0083] Table 2 properties of novel hydrocracking catalysts obtained from examples and comparative examples|[0084] |[0085] Example 6|[0086] The above-described catalyst A, B, C, D, E of the present invention was subjected to an activity evaluation test. The test uses a series process, and the properties of the raw oil are shown in Table 3. The operating conditions were as follows: hydrogen partial pressure 15.4MPa, hydrogen oil volume ratio 1200:1, the liquid time volume air speed is 1.2h -1, and the nitrogen content of the hydrorefining oil is controlled to be 10-15 mug/g. The results of the catalyst activity test are shown in Table 4.|[0087] Comparative example 4|[0088] Comparative example catalyst F, G, H was subjected to an activity evaluation test under the same conditions as in example 6, and the results of the catalyst activity test are shown in Table 4.|[0089] TABLE 3 Properties of raw oil|[0090] Iran reduced pressure wax oilDensity (20 ℃ C.)/(g/cm 3)0.9089Distillation range, DEG C303～547Nitrogen content/wt%0.135Sulfur content/wt%1.65Aromatic hydrocarbon/wt%38.5Condensation point, DEG C35|[0091] TABLE 4 evaluation results of catalyst Activity|[0092] |[0093] |[0094] The foregoing descriptions of specific exemplary embodiments of the present invention are presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application to thereby enable one skilled in the art to make and utilize the invention in various exemplary embodiments and with various modifications as are suited to the particular use contemplated. Any simple modifications, equivalent variations and modifications of the above-described exemplary embodiments should fall within the scope of the present invention. (CN116440942)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to a method for recycling a waste catalyst, in particular to a method for recycling a waste supported hydrocracking catalyst to prepare a novel hydrocracking catalyst.|BACKGROUND ART|[0002] The primary treatment of spent supported hydrogenation catalysts in the past has been landfills. However, the current production of waste supported hydrogenation catalysts in China exceeds 100000 tons each year, and the annual rapid increase of the catalyst still occurs at a rate of 4.4%, so that development of efficient technology for efficiently treating and cleaning and recycling toxic metal pollutants in the waste supported hydrogenation catalysts is needed.|[0003] CN107723468a discloses a comprehensive utilization system of waste catalyst. The system comprises an oil removal furnace, a rotary kiln, a four-stage countercurrent device, a stirring tank I, a plate and frame filter I, a precipitation tank I, a plate and frame filter II, a stirring tank II, a centrifugal machine I, ion exchange resin, an extraction device, a back extraction device, a precipitation tank II, a centrifugal machine II and a washing tank. The process can effectively recycle the useful components in the residual oil hydrogenation spent catalyst to obtain products such as industrial steam, nickel aluminum powder, ammonium metavanadate, high-purity molybdic acid, anhydrous sodium sulfate, distilled water and the like, and can obtain the high-purity molybdic acid without multiple separation processes, but the process is complex.|[0004] CN104628032B discloses a method for preparing high-purity ammonium metavanadate from waste catalyst. The method comprises the following steps: collecting the waste catalyst leaching solution by utilizing a leaching mode, filtering the leaching solution, then entering an ion exchange dephosphorization system, and utilizing resin to adsorb phosphorus and adsorb the phosphorus in the waste catalyst leaching solution; after dephosphorization, the molybdenum-vanadium-containing solution enters an ion exchange system, and molybdenum adsorption is carried out by using resin, so that molybdenum and vanadium are separated; pumping the vanadium-containing mother liquor after dephosphorization and molybdenum separation into a vanadium precipitation tank, and carrying out weak alkaline ammonium salt vanadium precipitation to obtain a high-purity ammonium metavanadate product. The method has the characteristics of short flow, simple process, energy conservation, environmental protection, high efficiency, low cost and the like, but can not make full use of things and can not fully mine the value of the waste hydrogenation catalyst.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the defects of the prior art, the invention provides a method for recycling a waste catalyst, which takes the waste supported hydrocracking catalyst as a raw material to prepare a novel hydrocracking catalyst, the method has the characteristics of simple preparation process, high metal recovery rate, low treatment cost and the like, and the obtained hydrocracking catalyst has good hydrogenation and cracking performances and better raw material adaptability.|[0006] The invention provides a method for recycling a waste catalyst, which comprises the following steps:|[0007] (1) Degreasing and decarbonizing the waste supported hydrocracking catalyst, and then crushing and sieving; |[0008] (2) Performing alkali treatment on the powder sieved in the step (1) by adopting an alkaline solution to obtain a molybdenum-containing aqueous solution and nickel-containing aluminum-silicon solid residues; |[0009] (3) Acid treatment is carried out on the solid residues containing nickel, aluminum and silicon obtained in the step (2) by adopting an acid solution, so as to obtain a nickel-containing aqueous solution and a silicon-aluminum material containing a Y-type molecular sieve; |[0010] (4) Adding an organic solvent and the silicon-aluminum material containing the Y molecular sieve obtained in the step (3) into a reaction kettle, stirring, adding an aluminum-containing acidic solution and an aluminum-containing alkaline solution, regulating the pH value to perform a first gel forming reaction, then sequentially and alternately adding the aluminum-containing acidic solution and the aluminum-containing alkaline solution, oscillating to form gel, and aging to obtain a catalyst carrier; |[0011] (5) And (3) impregnating the catalyst carrier obtained in the step (4) by using a solution containing an active metal component, and drying and roasting to obtain the novel hydrocracking catalyst. |[0012] In the method of the invention, in the step (1), the content of catalyst solids is 70-90% and the content of petroleum fraction is 10-30% by weight of the waste supported hydrocracking catalyst.|[0013] In the method of the present invention, in the step (1), the active metal supported by the waste supported hydrocracking catalyst includes molybdenum and nickel. The waste supported hydrocracking catalyst carrier comprises Al 2O3 -95% of Al 2O3 and 5-95% of Y-type molecular sieve by weight of the carrier.|[0014] In the method of the present invention, in the step (1), the oil removal is generally performed by a extraction method. The organic solvent adopted in the extraction is at least one of toluene, petroleum ether, ethanol and the like, the extraction temperature is 80-110 ℃, and the extraction time is 5-60 h.|[0015] In the method of the present invention, in the step (1), the carbon removal may be performed by a calcination method, wherein the calcination temperature is 500-700 ℃, preferably 600-650 ℃, and the calcination time is 2-48 hours, preferably 5-24 hours. The weight content of nickel oxide in the waste supported hydrocracking catalyst after oil removal and carbon removal is 2% -10%, the weight content of molybdenum oxide is 15% -50%, and the weight content of carbon is less than 1%.|[0016] In the process of the present invention, in the step (1), the particle size of the powder obtained after the pulverization and sieving is 200 to 400 mesh, preferably 300 to 400 mesh.|[0017] In the method of the invention, in the step (2), the alkaline solution is one or more of ammonia water, urea, ammonium carbonate, ammonium bicarbonate and the like, and the concentration of the alkaline solution is 5g/100 mL-100 g/100mL, preferably 10g/100 mL-90 g/100mL; the liquid-solid mass ratio of the alkaline solution to the powder sieved in the step (1) is 1:1 to 50:1, preferably 2:1 to 45:1.|[0018] In the method of the present invention, in the step (2), the conditions of the alkali treatment are as follows: the temperature is 100-400 ℃, preferably 150-350 ℃, the treatment time is 0.5-4.0 h, preferably 0.5-3.0 h, the pressure is 5-20 MPa, preferably 5-15 MPa, and the rate of heating to the treatment temperature is 5-25 ℃/min, preferably 5-10 ℃/min.|[0019] In the method, in the step (2), after alkali treatment, conventional filtration, washing and drying are carried out to obtain the molybdenum-containing water solution and the nickel-containing aluminum-silicon solid residue. Preferably, the leaching rate of the molybdenum oxide is 90-98%, preferably 95-98% after alkali treatment. The leaching rate of molybdenum oxide is the ratio of the mass of molybdenum in the molybdenum-containing aqueous solution to the mass of molybdenum in the waste supported hydrocracking catalyst, calculated as molybdenum oxide.|[0020] In the method of the present invention, in the step (3), the acidic solution is one or more of oxalic acid, carbonic acid, EDTA, acetic acid, sulfurous acid, etc., and the concentration thereof is 5g/100 mL-100 g/100mL, preferably 10g/100 mL-90 g/100mL. The liquid-solid mass ratio of the acidic compound in the acidic solution to the solid residue containing nickel-silicon-aluminum obtained in the step (2) is 1:1 to 50: 1, preferably 2:1 to 45:1.|[0021] In the method of the present invention, in the step (3), the conditions of the acid treatment are as follows: the temperature is 100-400 ℃, preferably 150-350 ℃, the treatment time is 0.5-4.0 h, preferably 0.5-3.0 h, the reaction pressure is 5-20 MPa, preferably 5-15 MPa, and the heating rate is 5-25 ℃/min, preferably 5-10 ℃/min. Preferably, the leaching rate of nickel oxide after acid treatment is 90% -98%, preferably 95% -98%. The leaching rate of nickel oxide is calculated as nickel oxide, and the ratio of the mass of nickel in the nickel-containing aqueous solution to the mass of nickel in the waste supported hydrocracking catalyst.|[0022] In the method, in the step (3), after acid treatment, the water solution containing nickel and the silicon-aluminum material containing the Y-type molecular sieve are obtained through conventional filtration, washing and drying.|[0023] In the method of the invention, in the step (3), the SiO 2/Al2O3 mol ratio of the silicon aluminum material containing the Y molecular sieve is 2:1 to 50: 1, preferably 2:1 to 25:1, the pore volume is 0.4-0.8 mL.g -1; the specific surface area is 650-750 m 2·g-1; the pore size may be less than 5nm, preferably 5 to 7nm.|[0024] In the method of the present invention, in the step (4), the organic solvent is one or more of alkane, alkene, organic alcohol, organic acid, etc., and further, the alkane is preferably at least one of pentane, hexane, dodecane, etc.; the olefin is preferably at least one of pentene, hexene and the like; the organic alcohol is at least one selected from organic monohydric alcohol and organic polyhydric alcohol, preferably at least one selected from n-hexanol, n-heptanol, pentaerythritol, glycerol, trimethylolethane, xylitol, sorbitol, etc.; the organic acid is at least one selected from aliphatic or aromatic carboxylic acids, such as benzoic acid, etc. The addition amount of the organic solvent is 1/5-1/2 of the actual effective use volume of the reaction kettle.|[0025] In the method of the invention, in the step (4), the concentration of the aluminum-containing alkaline salt solution calculated by alumina is 10-20 g/100mL; the concentration of the aluminum-containing acidic salt solution is 5-10 g/100mL calculated by alumina.|[0026] In the method of the present invention, in the step (4), the pH of the first glue is 7.0-9.0, the time is 3-15 min, and the temperature is 50-100 ℃, preferably 70-100 ℃;|[0027] The time of each glue forming in the swinging glue forming is 3-15 min, and the temperature of the swinging glue forming is 50-100 ℃, preferably 70-100 ℃. The pH value is adjusted to 2.0-3.0 during acid gel forming and 10.0-11.0 during alkaline gel forming, and the oscillating times are 2-8 times, preferably 3-5 times. The entire gelling process is carried out with stirring at a rate of 20 to 500rad/min, preferably 20 to 300rad/min. |[0028] In the method of the present invention, in the step (4), the aging conditions are as follows: the pH value is 7.0-9.0, the temperature is 50-100 ℃, preferably 70-100 ℃, and the time is 0.5-2.5 h, preferably 1.0-2.0 h.|[0029] In the method of the invention, in the step (4), after aging, the catalyst carrier is obtained through conventional filtration, drying and roasting.|[0030] In the process according to the invention, in step (5), the active metal is selected from one or more of the group VIII and/or group VIB metal elements, preferably one or more of tungsten, molybdenum, cobalt or nickel.|[0031] In the method of the present invention, in the step (5), the impregnation liquid containing active metal may be an aqueous solution containing molybdenum recovered in the step (2) or the step (3) or an aqueous solution containing nickel.|[0032] In the process of the present invention, in step (5), the impregnation may be carried out by impregnation means conventional in the art, such as isovolumetric impregnation, etc. The drying temperature is 100-200 ℃, preferably 120-150 ℃, the drying time is 2-10 h, the roasting temperature is 300-800 ℃, preferably 350-550 ℃, and the roasting time is 2.0-5.0 h, preferably 2.0-4.0 h.|[0033] The novel hydrocracking catalyst obtained by the invention takes R as the radius of catalyst particles, the silicon-aluminum material containing the Y-type molecular sieve is distributed in the range from the center to R/2-2R/3, and the aluminum oxide is distributed in the range from R/2-2R/3 to R.|[0034] The novel hydrocracking catalyst provided by the invention has the following properties: the pore volume is 1.5-2.0 mL.g -1; the specific surface area is 300-450 m 2·g-1; the pore diameter is not less than 10nm, preferably 15-25 nm; the particle size distribution is as follows: the proportion of the particle size less than 100 mu m is 0.5% -1%, the proportion of the particle size of 100-200 mu m is 2% -5%, and the proportion of the particle size more than 200 mu m is 90% -95%.|[0035] In the novel hydrocracking catalyst, the carrier content is 65-95% by weight of the catalyst, and the content of active metal calculated by oxide is 5-35%. Further, the content of the VIII group metal in an oxidation state is 3-30% and the content of the VIB group metal in an oxide is 0.5-5% based on the weight of the catalyst.|[0036] The invention also provides an application of the novel hydrocracking catalyst, the application is that the novel hydrocracking catalyst is applied to hydrocracking treatment of heavy inferior raw materials.|[0037] The heavy inferior raw materials comprise at least one of raw materials such as diesel oil, wax oil, residual oil, coal tar, coal liquefied oil and the like.|[0038] Compared with the prior art, the invention has the following advantages:|[0039] the method of the invention firstly carries out acid solution and alkaline solution treatment on the recovered waste hydrocracking catalyst, obtains the silicon-aluminum material which keeps the complete structure of the Y molecular sieve on the basis of recovering molybdenum and nickel solution, takes the material in the specific state as crystal nucleus, firstly mixes the crystal nucleus with organic solvent, forms alumina carrier material on the outer layer of the crystal nucleus by adopting pH swing neutralization mode, and the prepared catalyst has excellent hydrocracking performance and is suitable for processing inferior raw materials. |[0040] The method of the invention realizes the recycling of the waste hydrocracking catalyst, greatly reduces the production cost of the catalyst and improves the comprehensive utilization value of the waste catalyst.|DRAWINGS DESCRIPTION|[0041] FIG. 1 is an SEM image of a novel hydrocracking catalyst A obtained from example 1.|INVENTION MODE|Detailed Description|[0042] The present invention will be further described with reference to examples, but it should be understood that the scope of the present invention is not limited by the examples. In the present invention, percentages and percentages are by mass unless explicitly stated otherwise.|[0043] The SEM image of the invention is measured by a field emission scanning electron microscope (JSM 7500F), and the electron gun type is as follows: cold field emission gun, accelerating voltage: 0.1 kW-30 kW, resolution: 1.0nm (secondary electrons), 3.0nm (backscattered electrons), magnification: 25 to 1000000.|[0044] Example 1|[0045] The method comprises the steps of extracting 30% of oil-containing waste supported hydrocracking catalyst (the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve, the mass content of Al 2O3 is 80% and the mass content of the Y-type molecular sieve is 20%) with petroleum ether at 100 ℃ for 48 hours, roasting at 600 ℃ for 10 hours, wherein the obtained waste supported hydrocracking catalyst has the weight content of MoO 3 of 25.5%, the weight content of NiO of 8.5% and the carbon content of less than or equal to 0.9%, and then obtaining 300-400 mesh powder after crushing and screening.|[0046] Uniformly mixing an ammonium carbonate solution with the concentration of 25g/100mL and 100g of powder according to the liquid-solid mass ratio of 10:1, adding the mixture into an autoclave, heating to 200 ℃ at the heating rate of 5 ℃/min, reacting at the reaction pressure of 10.0MPa for 2.5 hours at the constant temperature, filtering and washing until the washing solution is neutral, and drying at 150 ℃ for 2 hours to obtain a molybdenum-containing solution and a nickel-silicon-aluminum-containing solid residue, wherein the leaching rate of MoO 3 is 98%.|[0047] Oxalic acid solution with the concentration of 20g/100mL and the solid residue containing nickel and silicon aluminum with the concentration of 75g are uniformly mixed according to the mass ratio of 10:1, the mixture is added into an autoclave, the temperature is raised to 250 ℃ at the heating rate of 10 ℃/min, the reaction pressure is 13.0MPa, the constant temperature time is 3 hours, and the mixture is filtered and washed until the washing solution is neutral, and the mixture is dried at 120 ℃ for 4 hours to obtain nickel-containing solution and silicon aluminum material A containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.8%.|[0048] Adding 50g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 5L of normal hexane into the reaction kettle, controlling the stirring speed to be 150rad/min, then adding a sodium metaaluminate solution with the concentration of 15g/100mL at the speed of 5mL/min, simultaneously adding an aluminum sulfate solution with the concentration of 5g/100mL, controlling the pH value to be 7.5, controlling the temperature to be 75 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 5g/100mL, stopping adding when the pH value is controlled to be 3.0, and stabilizing for 5 min; then adding 15g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to 11.0, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to 9.0, controlling the aging temperature to 100 ℃, aging for 2h, filtering, drying at 150 ℃ for 5h, and roasting at 500 ℃ for 4h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried at 120 ℃ for 3 hours and baked at 450 ℃ for 3 hours, so that the novel hydrocracking catalyst A is obtained, and the properties of the novel hydrocracking catalyst A are shown in table 2.|[0049] Example 2|[0050] The method comprises the steps of extracting a waste supported hydrocracking catalyst containing 25% of oil by using a petroleum ether and diethyl ether mixed solution with a volume ratio of 1:1 at 90 ℃ for 50 hours, roasting at 650 ℃ for 5 hours, wherein the waste supported hydrocracking catalyst contains 24.7% of MoO 3, 8.8% of NiO and less than or equal to 0.8% of carbon by weight, and the powder with 300-400 meshes is obtained after crushing and screening, wherein the waste supported hydrocracking catalyst carrier comprises Al 2O3 and Y-type molecular sieves, and the mass content of Al 2O3 is 95% and the mass content of Y-type molecular sieves is 5% based on the mass of the carrier.|[0051] Mixing 30g/100mL ammonia water solution and 250g of the powder according to a liquid-solid mass ratio of 15:1, uniformly adding the mixture into an autoclave, heating to 280 ℃ at a heating rate of 10 ℃/min, reacting at a reaction pressure of 13.0MPa for 3.0h, filtering and washing until a washing solution is neutral, and drying at 140 ℃ for 4h to obtain a molybdenum-containing solution and a nickel-silicon-containing solid residue, wherein the leaching rate of MoO 3 is 97%.|[0052] Uniformly mixing 15g/100mL of EDTA solution and 186g of nickel-containing silicon-aluminum solid residues according to a liquid-solid mass ratio of 18:1, adding the mixture into an autoclave, heating to 200 ℃ at a heating rate of 10 ℃/min, reacting at 15.0MPa for 2.5 hours at a constant temperature, filtering and washing until a washing solution is neutral, and drying at 150 ℃ for 3 hours to obtain a nickel-containing solution and a silicon-aluminum material B containing a Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 98%.|[0053] Crushing 100g of silicon-aluminum material containing the Y molecular sieve, adding 10L of n-hexylene alcohol into a reaction kettle, controlling the stirring speed to be 200rad/min, adding 12g/100mL of sodium metaaluminate solution at the speed of 10mL/min, simultaneously adding 10g/100mL of aluminum sulfate solution, controlling the pH value to be 8.5, controlling the temperature to be 90 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 10g/100mL, stopping adding when the pH value is controlled to be 2.0, and stabilizing for 5 min; then adding 12g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to be 10.0, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to 8.5, controlling the aging temperature to 100 ℃, aging for 1.5h, filtering, drying at 200 ℃ for 2h, and roasting at 500 ℃ for 4h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried at 150 ℃ for 2 hours and baked at 550 ℃ for 4 hours, so that the novel hydrocracking catalyst B is obtained, and the properties of the novel hydrocracking catalyst B are shown in table 2.|[0054] Example 3|[0055] The method comprises the steps of extracting a waste supported hydrocracking catalyst containing 28% of oil (the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve, the mass content of the Al 2O3 is 70% and the mass content of the Y-type molecular sieve is 30% based on the mass of the carrier) with toluene at 110 ℃ for 32 hours, roasting the waste supported hydrocracking catalyst at 630 ℃ for 12 hours, wherein the obtained waste supported hydrocracking catalyst has the MoO 3 weight content of 26.9%, the NiO weight content of 9.6% and the carbon content of less than or equal to 1.0%, and then obtaining 300-400 mesh powder after crushing and screening.|[0056] Uniformly mixing urea solution with the concentration of 45g/100mL and the 500g powder according to the mass ratio of liquid to solid of 20:1, adding the mixture into an autoclave, heating the autoclave to 300 ℃ at the heating rate of 8 ℃/min, reacting the mixture under the pressure of 15.0MPa, keeping the temperature for 2.0h, filtering and washing the mixture until the washing solution is neutral, and drying the mixture at 140 ℃ for 4h to obtain molybdenum-containing solution and nickel-silicon-containing solid residues, wherein the leaching rate of MoO 3 is 97.9%.|[0057] Acetic acid solution with the concentration of 30g/100mL and 379g of solid residue containing nickel-silicon-aluminum are evenly mixed according to the mass ratio of liquid to solid of 20:1, the mixture is added into an autoclave, the temperature is raised to 270 ℃ at the heating rate of 10 ℃/min, the reaction pressure is 14.6MPa, the constant temperature time is 2.0h, and the mixture is filtered and washed until washing liquid is neutral, and the mixture is dried at 150 ℃ for 5h to obtain nickel-containing solution and silicon-aluminum material C containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.9%.|[0058] Adding 300g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 20L of styrene into the reaction kettle, controlling the stirring speed to be 190rad/min, then adding 20g/100mL of sodium metaaluminate solution at a speed of 25mL/min, simultaneously adding 8g/100mL of aluminum sulfate solution, controlling the pH value to be 8.0, controlling the reaction temperature to be 95 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 8g/100mL, stopping adding when the pH value is controlled to be 2.0, and stabilizing for 5 min; then adding 20g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to be 10.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to be 7.5, controlling the aging temperature to be 95 ℃, aging for 2.0h, filtering, drying at 150 ℃ for 3h, and roasting at 550 ℃ for 5h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried for 5 hours at 140 ℃ and baked for 3 hours at 400 ℃, so that the novel hydrocracking catalyst C is obtained, and the properties of the novel hydrocracking catalyst C are shown in Table 2.|[0059] Example 4|[0060] The method comprises the steps of (1) adopting a volume ratio of a waste supported hydrocracking catalyst containing 20% of oil (the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve, wherein the mass content of Al 2O3 is 45% and the mass content of the Y-type molecular sieve is 55%) based on the mass of the carrier: 1, extracting toluene and petroleum ether at 110 ℃ for 36 hours, roasting at 650 ℃ for 8 hours, wherein the weight content of MoO 3 and the weight content of NiO are respectively 27.5% and less than or equal to 0.8%, and then crushing and screening to obtain 300-400 mesh powder.|[0061] Uniformly mixing 20g/100mL of ammonium carbonate solution and 200g of powder according to a liquid-solid mass ratio of 8:1, adding the mixture into an autoclave, heating to 220 ℃ at a heating rate of 10 ℃/min, reacting at a reaction pressure of 11.0MPa for 2.0h, filtering and washing until a washing solution is neutral, and drying at 150 ℃ for 3h to obtain a molybdenum-containing solution and a nickel-silicon-containing solid residue, wherein the leaching rate of MoO 3 is 98%.|[0062] Oxalic acid solution with the concentration of 25g/100mL and 175g of solid residues containing nickel and silicon aluminum are uniformly mixed according to the mass ratio of liquid to solid of 8:1, the mixture is added into an autoclave, the temperature is raised to 300 ℃ at the heating rate of 8 ℃/min, the reaction pressure is 15.0MPa, the constant temperature time is 2.5h, and the mixture is filtered and washed until the washing solution is neutral, and the mixture is dried at 180 ℃ for 2h to obtain nickel-containing solution and silicon aluminum material D containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.5%.|[0063] Adding 150g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 10L of hexane into the reaction kettle, controlling the stirring speed to be 150rad/min, then adding a sodium metaaluminate solution with the concentration of 20g/100mL at the speed of 10mL/min, simultaneously adding an aluminum sulfate solution with the concentration of 10g/100mL, controlling the pH value to be 7.0, controlling the reaction temperature to be 85 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 10g/100mL, stopping adding when the pH value is controlled to be 3.2, and stabilizing for 5 min; then adding 20g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to 11.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 4 times, adjusting the aging pH value to 9.0, controlling the aging temperature to 90 ℃, aging for 3h, filtering, drying at 120 ℃ for 5h, and baking at 500 ℃ for 3h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried for 3 hours at 120 ℃ and baked for 3 hours at 450 ℃ to obtain the novel hydrocracking catalyst D, wherein the properties of the novel hydrocracking catalyst D are shown in table 2.|[0064] Example 5|[0065] The method comprises the steps of (1) adopting a volume ratio of a waste supported hydrocracking catalyst containing 25% of oil (the carrier of the waste supported hydrocracking catalyst comprises Al 2O3 and a Y-type molecular sieve, wherein the mass content of Al 2O3 is 60% and the mass content of the Y-type molecular sieve is 40%) based on the mass of the carrier: 1, extracting toluene and diethyl ether at 110 ℃ for 38 hours, roasting at 620 ℃ for 8 hours, wherein the weight content of MoO 3 and the weight content of NiO are respectively 26.5% and 8.9% and less than or equal to 0.9%, and crushing and screening to obtain 300-400 mesh powder.|[0066] Uniformly mixing 40g/100mL ammonium carbonate solution and 300g of powder according to a liquid-solid mass ratio of 5:1, adding the mixture into an autoclave, heating to 250 ℃ at a heating rate of 10 ℃/min, reacting at a reaction pressure of 13.0MPa for 2.0h, filtering and washing until a washing solution is neutral, and drying at 130 ℃ for 4h to obtain a molybdenum-containing solution and a nickel-silicon-containing solid residue, wherein the leaching rate of MoO 3 is 97.5%.|[0067] Oxalic acid solution with the concentration of 15g/100mL and the solid residue containing nickel and silicon aluminum with the concentration of 269g are uniformly mixed according to the mass ratio of liquid to solid of 20:1, the mixture is added into an autoclave, the temperature is raised to 300 ℃ at the heating rate of 8 ℃/min, the reaction pressure is 15.0MPa, the constant temperature time is 2.5h, the mixture is filtered and washed until the washing solution is neutral, and the mixture is dried at 150 ℃ for 5h, so that nickel-containing solution and silicon aluminum material E containing Y molecular sieve are obtained, the properties of the nickel-containing solution and the silicon aluminum material E are shown in Table 1, and the leaching rate of NiO is 98.0%.|[0068] Adding 100g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 15L of dodecane into the reaction kettle, controlling the stirring speed to be 120rad/min, then adding a sodium metaaluminate solution with the concentration of 16g/100mL at the speed of 6mL/min, simultaneously adding an aluminum sulfate solution with the concentration of 15g/100mL, controlling the pH value to be 7.0, controlling the reaction temperature to be 85 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding an aluminum sulfate solution with the concentration of 15g/100mL, stopping adding when the pH value is controlled to be 3.0, and stabilizing for 5 min; then adding 16g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to 11.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to 10.0, controlling the aging temperature to 95 ℃, aging for 3.0h, filtering, drying at 170 ℃ for 2h, and roasting at 450 ℃ for 4h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried for 3 hours at 120 ℃ and baked for 3 hours at 450 ℃ to obtain the novel hydrocracking catalyst E, wherein the properties of the novel hydrocracking catalyst E are shown in table 2.|[0069] Comparative example 1|[0070] Adding an outsourced 350g Y molecular sieve (the properties of which are shown in table 1) into a reaction kettle, adding 15L of purified water into the reaction kettle, controlling the stirring speed to 190rad/min, controlling the reaction temperature to 95 ℃, then controlling the adding speed of a sodium metaaluminate solution with the concentration of 20g/100mL to 25mL/min, simultaneously adding an aluminum sulfate solution with the concentration of 8g/100mL, controlling the pH value to 8.0, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuously adding aluminum sulfate solution with the concentration of 8g/100mL, stopping adding when the pH value is controlled to be 2.0, and stabilizing for 5 min; then adding 20g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to be 10.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, adjusting the aging pH value to be 7.5 after swinging for 3 times, controlling the aging temperature to be 95 ℃, aging for 2.0h, filtering, drying at 150 ℃ for 3h, and roasting at 550 ℃ for 3h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried at 140 ℃ for 5 hours and baked at 400 ℃ for 3 hours, so that the hydrocracking catalyst F is obtained, and the properties of the hydrocracking catalyst F are shown in table 2.|[0071] Comparative example 2|[0072] The waste supported hydrocracking catalyst (same as in example 3) containing 28% of oil is extracted by toluene at 110 ℃ for 32 hours, and then baked at 630 ℃ for 12 hours, the weight content of MoO 3 of the obtained waste supported hydrocracking catalyst is 26.9%, the weight content of NiO is 9.6%, the carbon content is less than or equal to 1.0%, and then crushed and sieved to obtain 300-400 mesh powder.|[0073] Uniformly mixing urea solution with the concentration of 45g/100mL and the 500g powder according to the mass ratio of liquid to solid of 20:1, adding the mixture into an autoclave, heating the autoclave to 300 ℃ at the heating rate of 8 ℃/min, reacting the mixture under the pressure of 15.0MPa, keeping the temperature for 2.0h, filtering and washing the mixture until the washing solution is neutral, and drying the mixture at 140 ℃ for 4h to obtain molybdenum-containing solution and nickel-silicon-containing solid residues, wherein the leaching rate of MoO 3 is 97.9%.|[0074] Acetic acid solution with the concentration of 30g/100mL and 379g of solid residue containing nickel-silicon-aluminum are evenly mixed according to the mass ratio of liquid to solid of 20:1, the mixture is added into an autoclave, the temperature is raised to 270 ℃ at the heating rate of 10 ℃/min, the reaction pressure is 14.6MPa, the constant temperature time is 2.0h, and the mixture is filtered and washed until washing liquid is neutral, and the mixture is dried at 150 ℃ for 5h to obtain nickel-containing solution and silicon-aluminum material C containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.9%.|[0075] The molybdenum-containing solution and the nickel-containing solution are immersed to obtain a silicon-aluminum material G containing the Y molecular sieve, the silicon-aluminum material G is dried for 5 hours at 140 ℃ and baked for 3 hours at 400 ℃, and the hydrocracking catalyst G is obtained, and the properties of the hydrocracking catalyst G are shown in Table 2.|[0076] Comparative example 3|[0077] The waste supported hydrocracking catalyst (same as in example 3) containing 28% of oil is extracted by toluene at 110 ℃ for 32 hours, and then baked at 630 ℃ for 12 hours, the weight content of MoO 3 of the obtained waste supported hydrocracking catalyst is 26.9%, the weight content of NiO is 9.6%, the carbon content is less than or equal to 1.0%, and then crushed and sieved to obtain 300-400 mesh powder.|[0078] Uniformly mixing urea solution with the concentration of 45g/100mL and the 500g powder according to the mass ratio of liquid to solid of 20:1, adding the mixture into an autoclave, heating the autoclave to 300 ℃ at the heating rate of 8 ℃/min, reacting the mixture under the pressure of 15.0MPa, keeping the temperature for 2.0h, filtering and washing the mixture until the washing solution is neutral, and drying the mixture at 140 ℃ for 4h to obtain molybdenum-containing solution and nickel-silicon-containing solid residues, wherein the leaching rate of MoO 3 is 97.9%.|[0079] Acetic acid solution with the concentration of 30g/100mL and 379g of solid residue containing nickel-silicon-aluminum are evenly mixed according to the mass ratio of liquid to solid of 20:1, the mixture is added into an autoclave, the temperature is raised to 270 ℃ at the heating rate of 10 ℃/min, the reaction pressure is 14.6MPa, the constant temperature time is 2.0H, and the mixture is filtered and washed until washing liquid is neutral, and the mixture is dried at 150 ℃ for 5H to obtain nickel-containing solution and silicon-aluminum material H containing Y molecular sieve, wherein the property is shown in Table 1, and the leaching rate of NiO is 97.9%.|[0080] Adding 300g of the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding 20L of purified water into the reaction kettle, controlling the stirring speed to be 190rad/min, adding 20g/100mL of sodium metaaluminate solution at the speed of 25mL/min, simultaneously adding 8g/100mL of aluminum sulfate solution, controlling the pH value to be 8.0, controlling the reaction temperature to be 95 ℃, and stopping adding the sodium metaaluminate solution after the neutralization time is 5 min; continuing to add the aluminum sulfate solution with the concentration of 8g/100mL, stopping adding when the pH value is controlled to be 2.0, and stabilizing for 5 min; then adding 20g/100mL sodium metaaluminate solution, stopping adding when the pH value is controlled to be 10.5, stabilizing for 5min, adding aluminum sulfate solution and sodium metaaluminate solution as above, swinging for 3 times, adjusting the aging pH value to be 7.5, controlling the aging temperature to be 95 ℃, aging for 2.0h, filtering, drying at 150 ℃ for 3h, and roasting at 550 ℃ for 5h to obtain the required catalyst carrier. The obtained molybdenum-containing solution and nickel-containing solution are impregnated into the obtained carrier, and the carrier is dried at 140 ℃ for 5 hours and baked at 400 ℃ for 3 hours, so that the hydrocracking catalyst H is obtained, and the properties of the hydrocracking catalyst H are shown in table 2.|[0081] TABLE 1|[0082] |[0083] Table 2 properties of novel hydrocracking catalysts obtained from examples and comparative examples|[0084] |[0085] Example 6|[0086] The above-described catalyst A, B, C, D, E of the present invention was subjected to an activity evaluation test. The test uses a series process, and the properties of the raw oil are shown in Table 3. The operating conditions were as follows: hydrogen partial pressure 15.4MPa, hydrogen oil volume ratio 1200:1, the liquid time volume air speed is 1.2h -1, and the nitrogen content of the hydrorefining oil is controlled to be 10-15 mug/g. The results of the catalyst activity test are shown in Table 4.|[0087] Comparative example 4|[0088] Comparative example catalyst F, G, H was subjected to an activity evaluation test under the same conditions as in example 6, and the results of the catalyst activity test are shown in Table 4.|[0089] TABLE 3 Properties of raw oil|[0090] Iran reduced pressure wax oilDensity (20 ℃ C.)/(g/cm 3)0.9089Distillation range, DEG C303～547Nitrogen content/wt%0.135Sulfur content/wt%1.65Aromatic hydrocarbon/wt%38.5Condensation point, DEG C35|[0091] TABLE 4 evaluation results of catalyst Activity|[0092] |[0093] |[0094] The foregoing descriptions of specific exemplary embodiments of the present invention are presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application to thereby enable one skilled in the art to make and utilize the invention in various exemplary embodiments and with various modifications as are suited to the particular use contemplated. Any simple modifications, equivalent variations and modifications of the above-described exemplary embodiments should fall within the scope of the present invention. Family Number|(105754646)|105754646|Abstract|(CN116440942B B)|The invention discloses a method for recycling a waste catalyst . The method comprises the following steps : ( 1 ) carrying out oil removal , carbon removal , crushing and screening on the waste supported hydrocracking catalyst ; ( 2 ) carrying out alkali treatment by adopting an alkaline solution to obtain a molybdenum - containing aqueous solution and solid residues containing nickel , aluminum and silicon ; ( 3 ) carrying out acid treatment by adopting an acid solution to obtain a nickel - containing aqueous solution and a silicon - aluminum material containing the Y - type molecular sieve ; ( 4 ) adding an organic solvent and the silicon - aluminum material containing the Y molecular sieve into a reaction kettle , adding an aluminum - containing acidic solution and an aluminum - containing alkaline solution , carrying out a first gelling reaction , sequentially and alternately adding the aluminum - containing acidic solution and the aluminum - containing alkaline solution , and carrying out swing gelling and aging to obtain a catalyst carrier ; and ( 5 ) impregnating the catalyst carrier with a solution containing active metal components , drying , and roasting to obtain the novel hydrocracking catalyst . The hydrocracking catalyst obtained by the method is good in hydrogenation and cracking performance and has better raw material adaptability . |CPC codes|(CN116440942B B)|B01J - 029/16/6 |B01J - 037/02/07 |B01J - 037/02/13 |B01J - 038/02 |B01J - 038/48/5 |B01J - 038/50 |B01J - 038/62 |B01J - 038/64 |B01J - 038/68 |B01J - 2229/18 |B01J - 2229/42 |IPC codes|(CN116440942B B)|B01J - 029/16 |B01J - 037/02 |B01J - 038/02 |B01J - 038/48 |B01J - 038/50 |B01J - 038/62 |B01J - 038/64 |B01J - 038/68 | Basic materials chemistry|Chemical engineering B01J-029/16/6|B01J-037/02/07|B01J-037/02/13|B01J-038/02|B01J-038/48/5|B01J-038/50|B01J-038/62|B01J-038/64|B01J-038/68|B01J-2229/18|B01J-2229/42|C10G-047/20|Y02P-010/20 B01J-029/16/6|B01J-037/02/07|B01J-037/02/13|B01J-038/02|B01J-038/48/5|B01J-038/50|B01J-038/62|B01J-038/64|B01J-038/68|B01J-2229/18|B01J-2229/42|C10G-047/20|Y02P-010/20 B01J-029/16|B01J-037/02|B01J-038/02|B01J-038/48|B01J-038/50|B01J-038/62|B01J-038/64|B01J-038/68|C10G-047/20 B01J-029/16|B01J-037/02|B01J-038/02|B01J-038/48|B01J-038/50|B01J-038/62|B01J-038/64|B01J-038/68|C10G-047/20 CN111530494|CN112619658|CN111821995|WO2018161952|CN104549430|US6080226|US5077253|US5001096|CN102451744|CN101468317 CN111530494 90205845 WHO=Examiner SELF=N CAT=A|CN112619658 93541327 WHO=Examiner SELF=Y CAT=A|CN111821995 91192705 WHO=Examiner SELF=Y CAT=A|WO2018161952 76421758 WHO=Examiner SELF=N CAT=A|CN104549430 69216739 WHO=Examiner SELF=Y CAT=A|US6080226 43127108 WHO=Examiner SELF=N CAT=A|US5077253 42714469 WHO=Examiner SELF=N CAT=A|US5001096 69360 WHO=Examiner SELF=N CAT=A|CN102451744 7630364 WHO=Examiner SELF=Y|CN101468317 6792942 WHO=Examiner SELF=Y JIAO, WQ ET AL.: &quot;“Core-Shell Zeolite Y@γ-Al2O3 Nanorod Composites: Optimized Fluid Catalytic Cracking Catalyst Assembly for Processing Heavy Oil”&quot;, 《CHEMCATCHEM》, vol. 9, no. 13, 25 July 2017 (2017-07-25), pages 2574 - 2583, XP072440613, DOI: 10.1002/cctc.201700029 (Cat. A)|隋宝宽等: &quot;“渣油废催化剂回收制备拟薄水铝石”&quot;, 《石油化工高等学校学报》, vol. 32, no. 6, 31 December 2019 (2019-12-31), pages 8 - 13 (Cat. A) US5001096; US5077253; US6080226; CN104549430; CN111530494; CN111821995; CN112619658; WO2018161952; CN101468317; CN102451744 GRANTED (CN116440942)|GRANTED ALIVE (CN116440942)|ALIVE (CN116440942)|LEGAL DETAILS FOR CN116440942|Actual or expected expiration date=2042-01-06|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-01-06|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210008427|Application date=2022-01-06|Standardized application number=2022CN-0008427|Event publication date=2023-07-18|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN116440942|Publication stage code=A|Publication date=2023-07-18|Standardized publication number=CN116440942|Event publication date=2023-07-18|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-08-04|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-02-27|Event code=CN/TA01|Event group=Change of name or address Reassignment|Transfer of the patent application right or the patent right|FORMER APPLICANT:SINOPEC DALIAN RES INST PETROLEUM & PETROCHEMICALS FORMER APPLICANT:CHINA PETROLEUM & CHEMICAL CORP. APPLICANT:SINOPEC DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS CO., LTD. APPLICANT:CHINA PETROLEUM & CHEMICAL CORP.|Effective date of the event=2024-02-06|Event publication date=2024-10-01|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN116440942|Publication stage code=B|Publication date=2024-10-01|Standardized publication number=CN116440942B|Event publication date=2024-10-01|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN116440942)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQeICpiUQfzjRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000074628305&ekey=2044&xpn=CN116440942B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252B4yFlewA2I86lCOEp0RwS7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN116440942)|CN|(CN116440942)|CN (CN116440942)|NAME=CHINA PETROLEUM & CHEMICAL CORP. , COUNTRY=CN|(CN116440942)|NAME=CHINA PETROLEUM & CHEMICAL CORP. , COUNTRY=CN (CN116440942)|NAME=LÜ ZHENHUI|NAME=PENG CHONG|NAME=XUE DONG|NAME=ZHU HUIHONG|(CN116440942)|NAME=LÜ ZHENHUI|NAME=PENG CHONG|NAME=XUE DONG|NAME=ZHU HUIHONG 0 1 Titre: (CN116440942)|Method for recycling waste catalyst Résumé: (CN116440942)|The invention discloses a method for recycling a waste catalyst. The method comprises the following steps: (1) carrying out oil removal, carbon removal, crushing and screening on the waste supported hydrocracking catalyst; (2) carrying out alkali treatment by adopting an alkaline solution to obtain a molybdenum-containing aqueous solution and solid residues containing nickel, aluminum and silicon; (3) carrying out acid treatment by adopting an acid solution to obtain a nickel-containing aqueous solution and a silicon-aluminum material containing the Y-type molecular sieve; (4) adding an organic solvent and the silicon-aluminum material containing the Y molecular sieve into a reaction kettle, adding an aluminum-containing acidic solution and an aluminum-containing alkaline solution, carrying out a first gelling reaction, sequentially and alternately adding the aluminum-containing acidic solution and the aluminum-containing alkaline solution, and carrying out swing gelling and aging to obtain a catalyst carrier; and (5) impregnating the catalyst carrier with a solution containing active metal components, drying, and roasting to obtain the novel hydrocracking catalyst. The hydrocracking catalyst obtained by the method is good in hydrogenation and cracking performance and has better raw material adaptability. 50 Abstract gpt-4o-mini no The article focuses on recycling a waste catalyst and does not mention accelerated weathering, CO₂ capture, or related processes.
51 CN202111239939 CN202111239939 CN113755153 97504151 CN113755153 A 2021-12-07 [CN113755153] 2021-10-25 2021-10-25 2021-12-07 (CN113755153)|2023-04-25 (CN113755153)|Preparation method of propping agent for hazardous waste carbon sequestration and fracturing fluid (CN113755153)|The invention discloses a preparation method of a propping agent for hazardous waste carbon sequestration and fracturing fluid. The preparation method of the propping agent for hazardous waste carbon sequestration and fracturing fluid mainly comprises the steps of S1, crushing bauxite with the particle size of 350-500mm in a factory and raw materials, sieving, collecting the raw materials with the particle size of less than or equal to 6mm, and enabling the raw materials which do not meet the requirement to enter the crushing process again for crushing; S2, feeding the collected raw materials with the particle size less than or equal to 6 mm into a drying machine at the temperature of 60-90 DEG C to be dried, then enabling the raw materials, manganese powder, a fixing agent and a lubricating agent to pass through a batching station and enter a grinding system with a vortex powder concentrator to prepare raw material powder with the fineness being 400 meshes or above, adding water, and preparing the raw material powder into pellets with the qualified particle size. According to the invention, grinding is carried out after drying, and an efficient powder concentrator is matched to form a closed-loop system, so that the grinding efficiency is high, and meanwhile, the manganese powder, the fixing agent and the lubricating agent are added, so that the stability, the strength, the sealing property and the crushing resistance of a finished product are improved. HARBIN FUJIALONG TECHNOLOGY (CN113755153)|HARBIN FUJIALONG TECHNOLOGY CO., LTD. ([CN]) YANG BINGDONG|YAO SHUO|HU BENTAO (CN113755153)|YANG BINGDONG|YAO SHUO|HU BENTAO (CN113755153)|1. The preparation method of the proppant for the carbon sequestration and fracturing fluid by utilizing the hazardous waste is characterized by mainly comprising the following steps of:s1: crushing and sieving bauxite with the grain size of 350-500 mm and raw materials, collecting the raw materials with the grain size of less than or equal to 6mm, and crushing the raw materials which do not meet the requirement again in a crushing process;s2: the collected raw materials with the particle size of less than or equal to 6mm are sent into a dryer at the temperature of 60-90 ℃ for drying, then the raw materials, manganese powder, a fixing agent and a lubricating agent pass through a batching station and enter a grinding system with an eddy current powder concentrator to prepare raw material powder with the fineness of more than 400 meshes, and the raw material powder is prepared into spherical particles with qualified particle size after water is added;s3: then the mixture enters a rotary kiln for calcination after being screenedThe material balls are calcined in a rotary kiln with a certain inclination, the material balls roll towards the kiln head along with the rotation of the rotary kiln, meanwhile, the coal powder is sprayed into the kiln from the kiln head for combustion, the material balls are calcined into ceramsite sand with high strength in the rotary kiln, the calcined ceramsite sand is cooled by a single cooler, then the temperature of waste gas of the rotary kiln is dried for a second time, the waste gas is screened and cooled by a cylindrical screen, qualified different particle sizes are respectively packaged for standby, and unqualified ceramsite is returned to a grinding system.| (CN113755153)|According to the invention, bauxite which is a main material is firstly mined, the block size after mining is about 300-500 mm generally, and the bauxite containing a small amount of water is collected and stored, a crushing system consisting of a jaw crusher and a hammer crusher is firstly adopted for crushing when processing is required, the raw material with large particle size can be rapidly crushed and processed, the raw material with different particle sizes is screened after crushing, the particle size of the raw material is controlled to be less than or equal to 6mm through screening for multiple times, the raw material which does not reach the requirement is collected and reserved, and meanwhile, the raw material which reaches the requirement after crushing enters the crushing process again and is crushed, and the raw material which reaches the requirement after crushing is collected and used again.|In order to achieve the purpose, the invention adopts the following technical scheme:|The invention discloses a preparation method of a proppant for carbon sequestration and fracturing fluid by utilizing hazardous waste, which mainly comprises the following steps: s1: the bauxite with the incoming grain size of 350-500 mm and the raw material are crushed and sieved, the raw material with the grain size not larger than 6mm is collected, the raw material which does not meet the requirement enters the crushing process again and is crushed, and S2: the method comprises the steps of conveying collected raw materials with the particle size of less than or equal to 6mm into a dryer at 60-90 ℃ for drying, then enabling the raw materials, manganese powder, a fixing agent and a lubricating agent to enter a grinding system with an eddy current powder concentrator through a batching station to prepare raw material powder with the fineness of more than 400 meshes, adding water, and then enabling the raw material powder to be prepared into spherical particles with qualified particle sizes. The invention relates to the technical field of hazardous waste carbon sealing and fracturing fluid, in particular to a preparation method of a proppant for hazardous waste carbon sealing and fracturing fluid.| (CN113755153)|CARBON SEQUESTRATION(100,19)|FRACTURING FLUID(100,19)|PROPPANT(100,19)|HAZARDOUS WASTE(100,10)|UNQUALIFIED CERAMSITE(100,1)|CRUSHING(78,10)|BATCHING STATION(72,4)|POWDER CONCENTRATOR(71,3)|SIEVING BAUXITE(65,2)|HAMMER CRUSHER(64,1)|TRIETHYLENE TETRAMINE(55,6)|SPHERICAL PARTICLE(55,4)|CALCINED CERAMSITE SAND(54,4)|HAZARDOUS WASTE CARBON SEALING(53,2)|EDDY CURRENT POWDER CONCENTRATOR(52,3)|HAZARDOUS WASTE CARBON SEQUESTRATION(51,5)|MANGANESE POWDER(48,7)|GRINDING(44,9)|KILN HEAD(44,8)|BAUXITE(43,10)|ROTARY KILN(41,21)|FINENESS(39,4)|QUARTZ SAND(37,9)|COAL POWDER(37,5)|CARBON SEALING(33,4)|DRYER(29,5)|JAW CRUSHER(29,1)|INCLINATION(26,4)|RAW MATERIAL(25,35)|CYLINDRICAL SCREEN(25,4)|PARTICLE SIZE QUALIFICATION(25,4)|SCREENING(25,1)|MINING(24,1)|CALCINATION(23,6)|LUBRICATING AGENT(23,5)|POLYETHYLENE WAX(23,3)|STANDBY(23,2)|CERAMSITE SAND(22,8)|KILN(22,7)|MATERIAL BALL(20,9)|CRUSHING(20,2)|BARIUM CARBONATE(18,6)|COMBUSTION(18,6)|ROTARY KILN WASTE GAS(18,6)|EDDY CURRENT(18,3)|PARTICLE SIZE(17,16)|GRAIN SIZE(17,7)|ETHYLENEDIAMINE(17,3)|BENZENESULFONIC ACID(16,6)|SINGLE COOLER(16,4)|LUBRICANT(16,3)|WASTE GAS(15,8)|IRON ORE(15,6)|BENTONITE(15,3)|DOLOMITE(15,3)|METHYL SILICONE OIL(15,3)|INCOMING GRAIN SIZE(14,2)|RAW MEAL GRINDING TIME(14,1)|RAW MATERIAL POWDER(13,12)|GRANULARITY QUALIFICATION(13,2)|RAW MATERIAL COLLECTION(12,7)|M PHENYLENEDIAMINE(12,5)|UNQUALIFIED CERAMSITE PARTICLE(12,1)|PHOSPHORIC ACID(11,6)|UNQUALIFIED SPHERULITE(11,1)|GEOLOGICAL SEQUESTRATION(10,1)|GEOLOGY STRATUM(10,1)|OCEAN SEQUESTRATION(10,1)|UNQUALIFIED SPHERICAL PARTICLE(10,1)|VORTEX POWDER CONCENTRATOR(10,1)|ROTARY COOLER(9,2)|GEOLOGICAL ROCK STRATUM(9,1)|CYLINDRICAL SIEVE(7,2)|COAL SPRAYING PIPE(7,1)|RAW MEAL POWDER(7,1)|COATING POLYIMIDE RESIN(6,1)|LARGE PARTICLE SIZE(6,1)|HARDNESS(5,3)|CROCUS(5,2)|CURING TEMPERATURE(5,2)|BLOCK SIZE(5,1)|CARBON STORAGE PASSAGEWAY(5,1)|CRUSH RESISTANCE(5,1)|CRUSHING RESISTANCE(5,1)|FRACTURING FLUID CLOSURE(5,1)| (CN113755153)|1. The preparation method of the proppant for the carbon sequestration and fracturing fluid by utilizing the hazardous waste is characterized by mainly comprising the following steps of:|s1: crushing and sieving bauxite with the grain size of 350-500 mm and raw materials, collecting the raw materials with the grain size of less than or equal to 6mm, and crushing the raw materials which do not meet the requirement again in a crushing process;|s2: the collected raw materials with the particle size of less than or equal to 6mm are sent into a dryer at the temperature of 60-90 ℃ for drying, then the raw materials, manganese powder, a fixing agent and a lubricating agent pass through a batching station and enter a grinding system with an eddy current powder concentrator to prepare raw material powder with the fineness of more than 400 meshes, and the raw material powder is prepared into spherical particles with qualified particle size after water is added;|s3: then the mixture enters a rotary kiln for calcination after being screenedThe material balls are calcined in a rotary kiln with a certain inclination, the material balls roll towards the kiln head along with the rotation of the rotary kiln, meanwhile, the coal powder is sprayed into the kiln from the kiln head for combustion, the material balls are calcined into ceramsite sand with high strength in the rotary kiln, the calcined ceramsite sand is cooled by a single cooler, then the temperature of waste gas of the rotary kiln is dried for a second time, the waste gas is screened and cooled by a cylindrical screen, qualified different particle sizes are respectively packaged for standby, and unqualified ceramsite is returned to a grinding system.|2. The method for preparing the proppant for the carbon sequestration and fracturing fluid by using hazardous wastes according to claim 1, wherein the grinding time of the raw meal is 10 hours.|3. The method for preparing the proppant for the carbon sequestration and fracturing fluid by using the hazardous waste as claimed in claim 1, wherein the raw material powder is prepared into qualified spherulites with a granularity of 20-25 meshes.|4. The method for preparing the proppant for the hazardous waste carbon sequestration and fracturing fluid according to claim 1, wherein the raw material powder is prepared into a particle size and calcined at a temperature of 1300-1400 ℃.|5. The method for preparing the proppant for the use of hazardous waste carbon sequestration and fracturing fluid according to claim 1, wherein the raw meal is granulated and cooled in an environment with a temperature of 23-25 ℃.|6. The preparation method of the proppant for the carbon sequestration and fracturing fluid by using hazardous wastes according to claim 1, characterized in that the raw materials comprise, by weight: 25-30 parts of bauxite, 5-10 parts of iron ore, 12-18 parts of resin, 20-23 parts of bentonite, 13-15 parts of dolomite, 1-5 parts of barium carbonate and 20-30 parts of quartz sand.|7. The preparation method of the proppant for the hazardous waste carbon sequestration and fracturing fluid according to claim 1, wherein the manganese powder comprises the following components in parts by weight: 20-23 parts.|8. The preparation method of the proppant for the carbon sequestration and fracturing fluid by using hazardous wastes as claimed in claim 1, wherein the fixing agent comprises the following raw materials in proportion: 3-10 parts of m-phenylenediamine, 11-14 parts of benzenesulfonic acid, 6-13 parts of m-phenylenediamine, 4-12 parts of phosphoric acid and 5-10 parts of triethylene tetramine ethylenediamine.|9. The method for preparing the proppant for the use of hazardous waste carbon sequestration and fracturing fluid according to claim 1, wherein the lubricant is composed of methyl silicone oil and polyethylene wax. (CN113755153)|TECHNICAL FIELD|[0001] The invention relates to the technical field of hazardous waste carbon sealing and fracturing fluid, in particular to a preparation method of a proppant for hazardous waste carbon sealing and fracturing fluid.|BACKGROUND ART|[0002] Carbon capture and sequestration refers to a technology for collecting carbon dioxide generated by a power plant which emits a large amount of exhaust gas and storing the carbon dioxide by various methods to avoid the carbon dioxide from being emitted to the atmosphere, wherein the carbon sequestration comprises geological sequestration and ocean sequestration, wherein geological storage is realized by fracturing treatment through high closure pressure and low permeability of fracturing fluid to crack a geological rock stratum, a propping agent material is injected at the moment to form a storage channel for storage, and the carbon dioxide capture is divided into a plurality of methods such as capture before combustion and capture by combustion.|[0003] However, most of the existing proppants used for carbon sealing are products prepared from bauxite serving as a main raw material, and the products are low in strength and poor in sealing property and crushing resistance, so that the existing proppants are not suitable for carbon sealing used at present and do not have high stability for carbon sealing.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to solve the following defects in the prior art, and provides a method for preparing a proppant for carbon sequestration and fracturing fluid by using hazardous wastes, wherein the existing proppant for carbon sequestration is mostly a product prepared from bauxite serving as a main raw material, and the product is low in strength, poor in sealing property and poor in crushing resistance, so that the existing proppant is not suitable for carbon sequestration and does not have high stability for carbon sequestration.|[0005] In order to achieve the purpose, the invention adopts the following technical scheme:|[0006] the preparation method of the proppant for the hazardous waste carbon sequestration and fracturing fluid mainly comprises the following steps:|[0007] s1: crushing and sieving bauxite with the grain size of 350-500 mm, collecting raw materials with the grain size of less than or equal to 6mm, and crushing the raw materials which do not meet the requirement again in a crushing process;|[0008] s2: the collected raw materials with the particle size of less than or equal to 6mm are sent into a dryer at the temperature of 60-90 ℃ for drying, then the raw materials, manganese powder, a fixing agent and a lubricating agent pass through a batching station and enter a grinding system with an eddy current powder concentrator to prepare raw material powder with the fineness of more than 400 meshes, and the raw material powder is prepared into spherical particles with qualified particle size after water is added;|[0009] s3: then the mixture enters a rotary kiln for calcination after being screenedAnd then the mixture enters a rotary kiln with a certain inclination for calcination,the material balls roll towards the kiln head along with the rotation of the rotary kiln, meanwhile, the coal powder is sprayed into the kiln from the kiln head for combustion, the material balls are calcined into ceramsite sand with high strength in the rotary kiln, the calcined ceramsite sand is cooled by a single cooler, then the temperature of waste gas of the rotary kiln is dried for a second time and then is screened and cooled by a cylindrical screen, qualified different particle sizes are respectively packaged for later use, and unqualified ceramsite particles are returned to a grinding system.|[0010] Preferably, the grinding time of the raw meal powder is 10 hours.|[0011] Preferably, the raw material powder is prepared into qualified spherulites with the granularity of 20-25 meshes.|[0012] Preferably, the raw material powder is prepared into particles and calcined at the temperature of 1300-1400 ℃.|[0013] Preferably, the raw material powder is granulated and cooled in an environment with the temperature of 23-25 ℃.|[0014] Preferably, the weight ratio of the raw materials is as follows: 25-30 parts of bauxite, 5-10 parts of iron ore, 12-18 parts of resin, 20-23 parts of bentonite, 13-15 parts of dolomite, 1-5 parts of barium carbonate and 20-30 parts of quartz sand.|[0015] Preferably, the manganese powder comprises the following components in parts by weight: 20-23 parts.|[0016] Preferably, the fixing agent comprises the following raw materials in percentage by weight: 3-10 parts of m-phenylenediamine, 11-14 parts of benzenesulfonic acid, 6-13 parts of m-phenylenediamine, 4-12 parts of phosphoric acid and 5-10 parts of triethylene tetramine ethylenediamine.|[0017] Preferably, the lubricant is composed of methyl silicone oil and polyethylene wax.|[0018] Compared with the prior art, the invention has the beneficial effects that:|[0019] 1. the raw materials after collecting are dried, carry out the crocus and supporting high-efficient selection powder machine after the stoving, constitute closed system, the efficient of crocus like this, add manganese powder, fixative, emollient simultaneously, increase off-the-shelf stability, intensity, and leakproofness and anti crushing ability, can be better be used for the geology and store, make the geology stratum split after carrying out fracturing treatment through fracturing fluid high closure pressure hyposmosis, inject into the proppant material this moment, form the storage passageway of a carbon sealed up and store carbon dioxide.|[0020] 2. Meanwhile, when the collected raw materials with the particle size of less than or equal to 6mm are sent into a dryer at 60-90 ℃ to be dried and then stored, the temperature of waste gas of the rotary kiln can be used for secondary drying during storage, waste heat utilization is achieved, manufacturing cost is saved, and residual moisture in the materials is avoided.|[0021] 3. The calcined ceramsite sand is cooled by the single-cooler and then screened and cooled by the cylindrical screen, qualified different particle sizes are packaged for later use respectively, unqualified spherulites are returned to the grinding system, and therefore the effect of collecting different particle sizes is achieved, the different particle sizes are distinguished and used, meanwhile, the ceramsite sand has the characteristics of high temperature resistance, high pressure resistance and high strength, and the ceramsite sand can be effectively used in fracturing fluid carbon sequestration.|INVENTION MODE|Detailed Description|[0022] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.|[0023] A preparation method of a proppant for carbon sequestration and fracturing fluid by utilizing hazardous wastes mainly comprises the following steps:|[0024] s1: bauxite with the incoming grain size of 350-500 mm and raw materials are used, the bauxite is used as a main material for manufacturing a propping agent, and the weight ratio of the rest raw materials is as follows: 5-10 parts of iron ore, 12-18 parts of resin, 20-23 parts of bentonite, 13-15 parts of dolomite, 1-5 parts of barium carbonate and 20-30 parts of quartz sand, wherein the quartz sand is a non-metallic mineral substance and is a silicate mineral with hardness, wear resistance and stable chemical properties, the hardness and wear resistance of a raw material mixture can be increased, and the good performance of a geological carbon sealed storage environment can be guaranteed, when a single-layer resin coats the quartz sand, the type of the resin, the content of the resin, the curing temperature and the like have influence on the performance of a film coating supporting agent, the performance of the quartz sand is obviously improved after coating polyimide resin, when the curing temperature is 180 ℃, and the content of the resin is 8 wt%, the performance is best, the raw material with the particle size of less than or equal to 6mm is collected after crushing, the raw material with the particle size of less than or equal to 6mm is crushed again, the bauxite block serving as the raw material needs to control the particle size, the drying and grinding of the subsequent work are convenient;|[0025] s2: sending the collected raw materials with the particle size of less than or equal to 6mm into a dryer at the temperature of 60-90 ℃ for drying, and then passing the raw materials, manganese powder, a fixing agent and a lubricating agent through a batching station, wherein the manganese powder comprises the following components in parts by weight: 20 ~ 23 parts, manganese powder mainly improves intensity, hardness, elastic limit, wearability and the corrosion resistance etc. of composition, can play the better effect of sealing up the deposit to carbon dioxide in the carbon seals up the space to and can increase the stability of thick deposit structure, fixing agent raw materials ratio is: 3-10 parts of m-phenylenediamine, 11-14 parts of benzenesulfonic acid, 6-13 parts of meta-phenylenediamine, 4-12 parts of phosphoric acid and 5-10 parts of triethylene tetramine ethylenediamine, wherein a lubricant is composed of methyl silicone oil and polyethylene wax, raw material powder with the fineness of more than 400 meshes is prepared in a grinding system with a vortex powder concentrator, and the raw material powder is prepared into spherical particles with qualified particle size after water is added;|[0026] s3: then the mixture enters a rotary kiln for calcination after being screenedThe material ball is calcined in the rotary kiln with a certain inclination, the material ball rolls to the kiln head along with the rotation of the rotary kiln, and the coal powder is sprayed into the kiln from the kiln head for combustion, the coal powder burner can adopt a single-air-channel coal spraying pipe, is simple and reliable, has high primary air quantity, can also adopt a multi-air-channel burner, has the primary air quantity reduced to 8 percent of the air quantity required by the combustion of the coal powder, improves the secondary air quantity entering the kiln, has obvious energy-saving effect, is calcined into high-strength ceramsite sand in the rotary kiln, is calcined at the temperature of 1300-1400 ℃ when raw material powder is prepared into granularity, is cooled by a single cooler, is generally cooled by a rotary cooler, has simple and reliable operation, completely enters the kiln by secondary air of the cooler, is matched with the use of the multi-channel burner, can save a large amount of energy consumption, has low ceramsite sand temperature out of the cooler, and can be grabbed by hands, then the temperature of the waste gas of the rotary kiln is dried for a second time and then is screened and cooled by a cylindrical screen, so that the waste heat can be utilizedAnd the manufacturing cost is saved, the effect of recycling waste gas is achieved, the effect of drying incompletely dried materials again can be achieved, qualified different particle sizes are respectively packaged for standby, and unqualified spherical particles are returned to the grinding system.|[0027] According to the invention, bauxite which is a main material is firstly mined, the block size after mining is about 300-500 mm generally, and the bauxite containing a small amount of water is collected and stored, a crushing system consisting of a jaw crusher and a hammer crusher is firstly adopted for crushing when processing is required, the raw material with large particle size can be rapidly crushed and processed, the raw material with different particle sizes is screened after crushing, the particle size of the raw material is controlled to be less than or equal to 6mm through screening for multiple times, the raw material which does not reach the requirement is collected and reserved, and meanwhile, the raw material which reaches the requirement after crushing enters the crushing process again and is crushed, and the raw material which reaches the requirement after crushing is collected and used again.|[0028] Drying the collected raw materials, grinding the raw materials after drying, and matching with a high-efficiency powder selecting machine to form a closed-loop system, so that the grinding efficiency after drying is high, the working efficiency can be accelerated, manganese powder, a fixing agent and a lubricating agent are added in the processing process, the stability of a finished product is improved, hot air for drying the materials can come from waste gas of a rotary kiln, the waste heat is utilized, then raw material powder is made into spherulites with qualified granularity after water is added, meanwhile, the raw material powder is screened to be made into the spherulites with the qualified granularity of 20-25 meshes, the spherulites enter the rotary kiln with a certain inclination for calcination, the material balls roll towards a kiln head along with the rotation of the rotary kiln, meanwhile, the coal powder is sprayed into the kiln from the kiln head for combustion, the material balls are calcined into ceramsite sand with high strength in the rotary kiln, and the raw material powder is made into ceramsite with the granularity of 1300-1400 ℃ for calcinationThe calcined ceramsite sand is cooled by a single cooler, a rotary cooler is generally adopted for cooling the ceramsite sand, the operation is simple and reliable, secondary air of the cooler completely enters the kiln, a plurality of channel burners are matched for use, a large amount of energy consumption can be saved, the ceramsite sand discharged from the cooler is low in temperature and can be grabbed by hands, and then the temperature of waste gas of the rotary kiln is dried for the second timeThen sieving through a cylindrical sieve, cooling and then sieving through the cylindrical sieve.|[0029] The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention. (CN113755153)|TECHNICAL FIELD|[0001] The invention relates to the technical field of hazardous waste carbon sealing and fracturing fluid, in particular to a preparation method of a proppant for hazardous waste carbon sealing and fracturing fluid.|BACKGROUND ART|[0002] Carbon capture and sequestration refers to a technology for collecting carbon dioxide generated by a power plant which emits a large amount of exhaust gas and storing the carbon dioxide by various methods to avoid the carbon dioxide from being emitted to the atmosphere, wherein the carbon sequestration comprises geological sequestration and ocean sequestration, wherein geological storage is realized by fracturing treatment through high closure pressure and low permeability of fracturing fluid to crack a geological rock stratum, a propping agent material is injected at the moment to form a storage channel for storage, and the carbon dioxide capture is divided into a plurality of methods such as capture before combustion and capture by combustion.|[0003] However, most of the existing proppants used for carbon sealing are products prepared from bauxite serving as a main raw material, and the products are low in strength and poor in sealing property and crushing resistance, so that the existing proppants are not suitable for carbon sealing used at present and do not have high stability for carbon sealing.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to solve the following defects in the prior art, and provides a method for preparing a proppant for carbon sequestration and fracturing fluid by using hazardous wastes, wherein the existing proppant for carbon sequestration is mostly a product prepared from bauxite serving as a main raw material, and the product is low in strength, poor in sealing property and poor in crushing resistance, so that the existing proppant is not suitable for carbon sequestration and does not have high stability for carbon sequestration.|[0005] In order to achieve the purpose, the invention adopts the following technical scheme:|[0006] the preparation method of the proppant for the hazardous waste carbon sequestration and fracturing fluid mainly comprises the following steps:|[0007] s1: crushing and sieving bauxite with the grain size of 350-500 mm, collecting raw materials with the grain size of less than or equal to 6mm, and crushing the raw materials which do not meet the requirement again in a crushing process;|[0008] s2: the collected raw materials with the particle size of less than or equal to 6mm are sent into a dryer at the temperature of 60-90 ℃ for drying, then the raw materials, manganese powder, a fixing agent and a lubricating agent pass through a batching station and enter a grinding system with an eddy current powder concentrator to prepare raw material powder with the fineness of more than 400 meshes, and the raw material powder is prepared into spherical particles with qualified particle size after water is added;|[0009] s3: then the mixture enters a rotary kiln for calcination after being screenedAnd then the mixture enters a rotary kiln with a certain inclination for calcination,the material balls roll towards the kiln head along with the rotation of the rotary kiln, meanwhile, the coal powder is sprayed into the kiln from the kiln head for combustion, the material balls are calcined into ceramsite sand with high strength in the rotary kiln, the calcined ceramsite sand is cooled by a single cooler, then the temperature of waste gas of the rotary kiln is dried for a second time and then is screened and cooled by a cylindrical screen, qualified different particle sizes are respectively packaged for later use, and unqualified ceramsite particles are returned to a grinding system.|[0010] Preferably, the grinding time of the raw meal powder is 10 hours.|[0011] Preferably, the raw material powder is prepared into qualified spherulites with the granularity of 20-25 meshes.|[0012] Preferably, the raw material powder is prepared into particles and calcined at the temperature of 1300-1400 ℃.|[0013] Preferably, the raw material powder is granulated and cooled in an environment with the temperature of 23-25 ℃.|[0014] Preferably, the weight ratio of the raw materials is as follows: 25-30 parts of bauxite, 5-10 parts of iron ore, 12-18 parts of resin, 20-23 parts of bentonite, 13-15 parts of dolomite, 1-5 parts of barium carbonate and 20-30 parts of quartz sand.|[0015] Preferably, the manganese powder comprises the following components in parts by weight: 20-23 parts.|[0016] Preferably, the fixing agent comprises the following raw materials in percentage by weight: 3-10 parts of m-phenylenediamine, 11-14 parts of benzenesulfonic acid, 6-13 parts of m-phenylenediamine, 4-12 parts of phosphoric acid and 5-10 parts of triethylene tetramine ethylenediamine.|[0017] Preferably, the lubricant is composed of methyl silicone oil and polyethylene wax.|[0018] Compared with the prior art, the invention has the beneficial effects that:|[0019] 1. the raw materials after collecting are dried, carry out the crocus and supporting high-efficient selection powder machine after the stoving, constitute closed system, the efficient of crocus like this, add manganese powder, fixative, emollient simultaneously, increase off-the-shelf stability, intensity, and leakproofness and anti crushing ability, can be better be used for the geology and store, make the geology stratum split after carrying out fracturing treatment through fracturing fluid high closure pressure hyposmosis, inject into the proppant material this moment, form the storage passageway of a carbon sealed up and store carbon dioxide.|[0020] 2. Meanwhile, when the collected raw materials with the particle size of less than or equal to 6mm are sent into a dryer at 60-90 ℃ to be dried and then stored, the temperature of waste gas of the rotary kiln can be used for secondary drying during storage, waste heat utilization is achieved, manufacturing cost is saved, and residual moisture in the materials is avoided.|[0021] 3. The calcined ceramsite sand is cooled by the single-cooler and then screened and cooled by the cylindrical screen, qualified different particle sizes are packaged for later use respectively, unqualified spherulites are returned to the grinding system, and therefore the effect of collecting different particle sizes is achieved, the different particle sizes are distinguished and used, meanwhile, the ceramsite sand has the characteristics of high temperature resistance, high pressure resistance and high strength, and the ceramsite sand can be effectively used in fracturing fluid carbon sequestration.|INVENTION MODE|Detailed Description|[0022] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.|[0023] A preparation method of a proppant for carbon sequestration and fracturing fluid by utilizing hazardous wastes mainly comprises the following steps:|[0024] s1: bauxite with the incoming grain size of 350-500 mm and raw materials are used, the bauxite is used as a main material for manufacturing a propping agent, and the weight ratio of the rest raw materials is as follows: 5-10 parts of iron ore, 12-18 parts of resin, 20-23 parts of bentonite, 13-15 parts of dolomite, 1-5 parts of barium carbonate and 20-30 parts of quartz sand, wherein the quartz sand is a non-metallic mineral substance and is a silicate mineral with hardness, wear resistance and stable chemical properties, the hardness and wear resistance of a raw material mixture can be increased, and the good performance of a geological carbon sealed storage environment can be guaranteed, when a single-layer resin coats the quartz sand, the type of the resin, the content of the resin, the curing temperature and the like have influence on the performance of a film coating supporting agent, the performance of the quartz sand is obviously improved after coating polyimide resin, when the curing temperature is 180 ℃, and the content of the resin is 8 wt%, the performance is best, the raw material with the particle size of less than or equal to 6mm is collected after crushing, the raw material with the particle size of less than or equal to 6mm is crushed again, the bauxite block serving as the raw material needs to control the particle size, the drying and grinding of the subsequent work are convenient;|[0025] s2: sending the collected raw materials with the particle size of less than or equal to 6mm into a dryer at the temperature of 60-90 ℃ for drying, and then passing the raw materials, manganese powder, a fixing agent and a lubricating agent through a batching station, wherein the manganese powder comprises the following components in parts by weight: 20 ~ 23 parts, manganese powder mainly improves intensity, hardness, elastic limit, wearability and the corrosion resistance etc. of composition, can play the better effect of sealing up the deposit to carbon dioxide in the carbon seals up the space to and can increase the stability of thick deposit structure, fixing agent raw materials ratio is: 3-10 parts of m-phenylenediamine, 11-14 parts of benzenesulfonic acid, 6-13 parts of meta-phenylenediamine, 4-12 parts of phosphoric acid and 5-10 parts of triethylene tetramine ethylenediamine, wherein a lubricant is composed of methyl silicone oil and polyethylene wax, raw material powder with the fineness of more than 400 meshes is prepared in a grinding system with a vortex powder concentrator, and the raw material powder is prepared into spherical particles with qualified particle size after water is added;|[0026] s3: then the mixture enters a rotary kiln for calcination after being screenedThe material ball is calcined in the rotary kiln with a certain inclination, the material ball rolls to the kiln head along with the rotation of the rotary kiln, and the coal powder is sprayed into the kiln from the kiln head for combustion, the coal powder burner can adopt a single-air-channel coal spraying pipe, is simple and reliable, has high primary air quantity, can also adopt a multi-air-channel burner, has the primary air quantity reduced to 8 percent of the air quantity required by the combustion of the coal powder, improves the secondary air quantity entering the kiln, has obvious energy-saving effect, is calcined into high-strength ceramsite sand in the rotary kiln, is calcined at the temperature of 1300-1400 ℃ when raw material powder is prepared into granularity, is cooled by a single cooler, is generally cooled by a rotary cooler, has simple and reliable operation, completely enters the kiln by secondary air of the cooler, is matched with the use of the multi-channel burner, can save a large amount of energy consumption, has low ceramsite sand temperature out of the cooler, and can be grabbed by hands, then the temperature of the waste gas of the rotary kiln is dried for a second time and then is screened and cooled by a cylindrical screen, so that the waste heat can be utilizedAnd the manufacturing cost is saved, the effect of recycling waste gas is achieved, the effect of drying incompletely dried materials again can be achieved, qualified different particle sizes are respectively packaged for standby, and unqualified spherical particles are returned to the grinding system.|[0027] According to the invention, bauxite which is a main material is firstly mined, the block size after mining is about 300-500 mm generally, and the bauxite containing a small amount of water is collected and stored, a crushing system consisting of a jaw crusher and a hammer crusher is firstly adopted for crushing when processing is required, the raw material with large particle size can be rapidly crushed and processed, the raw material with different particle sizes is screened after crushing, the particle size of the raw material is controlled to be less than or equal to 6mm through screening for multiple times, the raw material which does not reach the requirement is collected and reserved, and meanwhile, the raw material which reaches the requirement after crushing enters the crushing process again and is crushed, and the raw material which reaches the requirement after crushing is collected and used again.|[0028] Drying the collected raw materials, grinding the raw materials after drying, and matching with a high-efficiency powder selecting machine to form a closed-loop system, so that the grinding efficiency after drying is high, the working efficiency can be accelerated, manganese powder, a fixing agent and a lubricating agent are added in the processing process, the stability of a finished product is improved, hot air for drying the materials can come from waste gas of a rotary kiln, the waste heat is utilized, then raw material powder is made into spherulites with qualified granularity after water is added, meanwhile, the raw material powder is screened to be made into the spherulites with the qualified granularity of 20-25 meshes, the spherulites enter the rotary kiln with a certain inclination for calcination, the material balls roll towards a kiln head along with the rotation of the rotary kiln, meanwhile, the coal powder is sprayed into the kiln from the kiln head for combustion, the material balls are calcined into ceramsite sand with high strength in the rotary kiln, and the raw material powder is made into ceramsite with the granularity of 1300-1400 ℃ for calcinationThe calcined ceramsite sand is cooled by a single cooler, a rotary cooler is generally adopted for cooling the ceramsite sand, the operation is simple and reliable, secondary air of the cooler completely enters the kiln, a plurality of channel burners are matched for use, a large amount of energy consumption can be saved, the ceramsite sand discharged from the cooler is low in temperature and can be grabbed by hands, and then the temperature of waste gas of the rotary kiln is dried for the second timeThen sieving through a cylindrical sieve, cooling and then sieving through the cylindrical sieve.|[0029] The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention. Family Number|(97504151)|97504151|Abstract|(CN113755153 A)|The invention discloses a preparation method of a propping agent for hazardous waste carbon sequestration and fracturing fluid . The preparation method of the propping agent for hazardous waste carbon sequestration and fracturing fluid mainly comprises the steps of S1 , crushing bauxite with the particle size of 350-500 mm in a factory and raw materials , sieving , collecting the raw materials with the particle size of less than or equal to 6 mm , and enabling the raw materials which do not meet the requirement to enter the crushing process again for crushing ; S2 , feeding the collected raw materials with the particle size less than or equal to 6 mm into a drying machine at the temperature of 60-90 DEG C to be dried , then enabling the raw materials , manganese powder , a fixing agent and a lubricating agent to pass through a batching station and enter a grinding system with a vortex powder concentrator to prepare raw material powder with the fineness being 400 meshes or above , adding water , and preparing the raw material powder into pellets with the qualified particle size . According to the invention , grinding is carried out after drying , and an efficient powder concentrator is matched to form a closed - loop system , so that the grinding efficiency is high , and meanwhile , the manganese powder , the fixing agent and the lubricating agent are added , so that the stability , the strength , the sealing property and the crushing resistance of a finished product are improved . |CPC codes|(CN113755153 A)|C01B - 032/50 |IPC codes|(CN113755153 A)|C01B - 032/50 |Title|(CN113755153 A)|Preparation method of propping agent for hazardous waste carbon sequestration and fracturing fluid | Basic materials chemistry|Materials, metallurgy C01B-032/50|C09K-008/80 C01B-032/50|C09K-008/80 C01B-032/50|C09K-008/80 C01B-032/50|C09K-008/80 CN109880611|CN103194204|CN102352241|CN109777395|CN109337669|CN108706960|CN102732245|US20070023187 CN109880611 84872104 WHO=Examiner SELF=N CAT=Y|CN103194204 45591991 WHO=Examiner SELF=N CAT=Y|CN102352241 7564589 WHO=Examiner SELF=N CAT=Y|CN109777395 84559966 WHO=Examiner SELF=N CAT=A|CN109337669 83438844 WHO=Examiner SELF=N CAT=A|CN108706960 81759847 WHO=Examiner SELF=N CAT=A|CN102732245 7903880 WHO=Examiner SELF=N CAT=A|US20070023187 1808874 WHO=Examiner SELF=N CAT=A 李小刚等: &quot;压裂用低密度支撑剂研究进展和发展趋势&quot;, 《硅酸盐通报》 (Cat. A) US20070023187; CN102352241; CN102732245; CN103194204; CN108706960; CN109337669; CN109777395; CN109880611 REVOKED (CN113755153)|REVOKED DEAD (CN113755153)|DEAD (CN113755153)|LEGAL DETAILS FOR CN113755153|Actual or expected expiration date=2023-04-25|Legal state=DEAD|Status=REVOKED|Event publication date=2021-10-25|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202111239939|Application date=2021-10-25|Standardized application number=2021CN-1239939|Event publication date=2021-12-07|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN113755153|Publication stage code=A|Publication date=2021-12-07|Standardized publication number=CN113755153|Event publication date=2021-12-07|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2021-12-24|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-04-25|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSeKUk3Tr6C2Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000060289813&ekey=1850&xpn=CN113755153&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=j5VmhpWuDwaLZI4PQo3BAJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN113755153)|CN (CN113755153)|NAME=HARBIN FUJIALONG TECHNOLOGY CO., LTD. , COUNTRY=CN (CN113755153)|NAME=YANG BINGDONG|NAME=YAO SHUO|NAME=HU BENTAO 0 1 Titre: (CN113755153)|Preparation method of propping agent for hazardous waste carbon sequestration and fracturing fluid Résumé: (CN113755153)|The invention discloses a preparation method of a propping agent for hazardous waste carbon sequestration and fracturing fluid. The preparation method of the propping agent for hazardous waste carbon sequestration and fracturing fluid mainly comprises the steps of S1, crushing bauxite with the particle size of 350-500mm in a factory and raw materials, sieving, collecting the raw materials with the particle size of less than or equal to 6mm, and enabling the raw materials which do not meet the requirement to enter the crushing process again for crushing; S2, feeding the collected raw materials with the particle size less than or equal to 6 mm into a drying machine at the temperature of 60-90 DEG C to be dried, then enabling the raw materials, manganese powder, a fixing agent and a lubricating agent to pass through a batching station and enter a grinding system with a vortex powder concentrator to prepare raw material powder with the fineness being 400 meshes or above, adding water, and preparing the raw material powder into pellets with the qualified particle size. According to the invention, grinding is carried out after drying, and an efficient powder concentrator is matched to form a closed-loop system, so that the grinding efficiency is high, and meanwhile, the manganese powder, the fixing agent and the lubricating agent are added, so that the stability, the strength, the sealing property and the crushing resistance of a finished product are improved. 48 Abstract gpt-4o-mini no The article focuses on a preparation method for a propping agent related to hazardous waste carbon sequestration and fracturing fluid, which does not align with the central topic of accelerated weathering or enhanced weathering for CO₂ capture.
52 CN201711461775 CN201711461775 CN109967036|CN109967036 85114797 CN109967036 B 2021-03-09 [CN109967036B]|CN109967036 A 2019-07-05 [CN109967036] 2017-12-28 2017-12-28 2021-03-09|2019-07-05 (CN109967036B)|2021-03-09 (CN109967036)|2037-12-28 (CN109967036)|Preparation method of sulfydryl modified activated carbon for removing malodor (CN109967036)|The invention provides a preparation method of thiol-modified activated carbon for removal of stink. The method includes the steps of: 1) crushing activated carbon to prepare activated carbon powder;2) mixing p-toluenethiol, thiourea, formaldehyde and water, and then conducting heating and stirring to obtain a thiol pre-polymerized modified solution; 3) conducting modification treatment on the activated carbon powder with the thiol pre-polymerized modified solution to obtain modified activated carbon; and 4) drying the modified activated carbon and then conducting heat treatment to obtain theneeded thiol-modified activated carbon. The invention further provides the thiol-modified activated carbon prepared by the method and application thereof. The preparation method of the thiol-modifiedactivated carbon for removal of stink provided by the invention can acquire thiol-modified activated carbon with uniformly distributed and adjustable thiol, thus further enhancing the stink removal efficiency of the modified activated carbon. The thiol-modified activated carbon is suitable for purification treatment of malodorous gases containing ammonia amino, ammonia aldehyde group, ammonia hydroxyl, ammonia carboxyl or ammonia phenol components. BAIMEI SMART TECHNOLOGY SHANGHAI (CN109967036)|BIOMINTEC ENVIRONMENT TECH SHANGHAI CO LTD ([CN])|(CN109967036)|BIOMINTEC ENVIRONMENT TECH SHANGHAI CO LTD ([CN]) XU QIAN|LI JUN (CN109967036)|XU QIAN|LI JUN|(CN109967036)|XU QIAN|LI JUN (CN109967036)|XU YILIN;JZMC PATENT AND TRADEMARK LAW OFFICE|Reg. Nb: 31219 (CN109967036)|Because the odor threshold of the malodorous substances is low, the sensory quantity (odor intensity) of people is in direct proportion to the logarithm of the stimulation quantity of the human olfactory sensation, the components are complex and have the characteristics of time interval, regionality and seasonality, the pollution events are increased day by day, and the treatment and management difficulty is increased more and more.|Compared with the activated carbon adsorption method, the chemical deodorization method needs to be provided with more auxiliary facilities such as a liquid medicine storage device, a liquid medicine conveying device, a discharging device and the like, has more complex operation management and higher operation cost, and has lower efficiency because the odor which does not react with the liquid medicine is difficult to remove.|The malodorous pollutants not only cause adverse psychological effects to people, but also cause damages to the respiratory system, the digestive system, the cardiovascular and cerebrovascular systems, the endocrine system and the nervous system of human bodies to different degrees, and some malodorous pollutants can also generate oxidation reaction and photochemical reaction in troposphere atmosphere, thereby playing an important role in acid rain and photochemical smog pollution.| (CN109967036)|1. A preparation method of sulfydryl modified activated carbon comprises the following steps:1) crushing the activated carbon to prepare activated carbon powder;2) mixing p-methyl thiophenol, thiourea, formaldehyde and water, heating and stirring to prepare a sulfydryl prepolymerization modified solution;3) modifying the active carbon powder prepared in the step 1) by using the sulfhydryl prepolymerization modification solution prepared in the step 2) to prepare modified active carbon;4) drying the modified activated carbon prepared in the step 3), and then carrying out heat treatment to obtain the required sulfydryl modified activated carbon;in the step 2), the preparation process of the sulfhydryl prepolymerization modification solution comprises the following steps:A) mixing p-methyl thiophenol, formaldehyde and water, and heating and stirring to obtain a first prepolymer solution;B) mixing thiourea, formaldehyde and water, and heating and stirring to prepare a second prepolymer solution;C) cooling and mixing the first prepolymer solution prepared in the step A) and the second prepolymer solution prepared in the step B) to obtain a total prepolymer solution, and diluting the total prepolymer solution with water to obtain a sulfhydryl prepolymerization modified solution;the preparation process of the mercapto prepolymerization modification liquid comprises any one or more of the following conditions:A1) in the step A), the molar ratio of p-methylthiophenol to formaldehyde is 1: 1.5-2.5;A2) in the step A), the volume ratio of the water to the formaldehyde is 1-10: 1-2;A3) in the step B), the molar ratio of the thiourea to the formaldehyde is 1: 1.5-2.5;A4) in the step B), the volume ratio of the water to the formaldehyde is 1-10: 1-2;A5) in the step C), the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.2-0.8: 1.| (CN109967036)|In view of the above-mentioned shortcomings of the prior art, the present invention aims to provide a method for preparing a mercapto activated carbon with uniform distribution of mercapto groups and adjustable content of mercapto functional groups, so as to solve the problem of lack of an activated carbon with high efficiency for removing malodors in the prior art. To achieve the above and other related objects, there is provided, in a first aspect of the present invention, a method for preparing mercapto-modified activated carbon for removing malodor, comprising the steps of:|The invention provides a preparation method of sulfhydryl modified activated carbon for removing malodor, which comprises the following steps: 1) crushing the activated carbon to prepare activated carbon powder; 2) mixing p-methyl thiophenol, thiourea, formaldehyde and water, heating and stirring to prepare a sulfydryl prepolymerization modified solution; 3) carrying out modification treatment on the activated carbon powder by using the sulfydryl prepolymerization modification liquid to prepare modified activated carbon; 4) and drying the modified activated carbon, and then carrying out heat treatment to obtain the required sulfydryl modified activated carbon. The invention further provides the sulfhydryl modified activated carbon prepared by the method and application thereof.|The invention provides sulfydryl modified activated carbon, which is prepared by the method. The third aspect of the invention provides the application of the sulfhydryl modified activated carbon in the purification treatment of ammonia-containing malodorous gas.| (CN109967036)|ACTIVATED CARBON MODIFICATION(100,51)|SULFYDRYL MODIFIED ACTIVATED CARBON(100,25)|MALODOR REMOVAL(100,8)|SULFYDRYL PREPOLYMERIZATION MODIFICATION(100,1)|MALODOROUS POLLUTANT(94,2)|SULFYDRYL PREPOLYMERIZATION(85,33)|MERCAPTO PREPOLYMERIZATION MODIFICATION(85,1)|HUMAN OLFACTORY SENSATION STIMULATION(69,1)|MERCAPTOMODIFIED ACTIVATED CARBON(65,17)|SULFHYDRYL PREPOLYMERIZATION MODIFICATION SOLUTION(63,5)|PHOTOCHEMICAL SMOG POLLUTION(58,1)|PREPOLYMER SOLUTION(55,46)|SULFHYDRYL PREPOLYMERIZATION(53,8)|FORMALDEHYDE(51,48)|HUMAN OLFACTORY SENSATION(45,1)|TROPOSPHERE ATMOSPHERE(45,1)|AUXILIARY FACILITY(43,1)|SULFHYDRYL MODIFIED ACTIVATED CARBON(42,4)|MALODOROUS SUBSTANCE(40,2)|MANAGEMENT DIFFICULTY(37,1)|ODOR INTENSITY(37,1)|PURIFICATION TREATMENT(34,3)|MIXING THIOUREA(34,2)|MALODOROUS GAS(33,13)|MIXING P THIOCRESOL(33,11)|MERCAPTO PREPOLYMERIZATION MODIFICATION SOLUTION(33,1)|THIOUREA(31,18)|TOTAL PREPOLYMER SOLUTION(30,25)|ACTIVATED CARBON(29,63)|CONTAMINATION(28,1)|MERCAPTOGROUP PREPOLYMERIZATION MASS RATIO(28,1)|ACTIVATED CARBON POWDER(27,31)|REGIONALITY(27,1)|SEASONALITY(27,1)|LOGARITHM(26,1)|MOLAR RATIO(25,17)|DISCHARGE(25,1)|ACTIVATED CARBON ADSORPTION(24,1)|ADJUSTABLE MERCAPTO GROUP(24,1)|MERCAPTO ACTIVATED CARBON(24,1)|MERCAPTO GROUP UNIFORM DISTRIBUTION(24,1)|UNIFORM DISTRIBUTION(24,1)|DEODORIZATION(23,5)|LIQUID PHARMACEUTICAL(22,2)|SATURATED ADSORPTION CAPACITY(21,12)|ABSOLUTE ALCOHOL(20,2)|ADJUSTABLE CONTENT(20,2)|MERCAPTO GROUP(20,2)|ODOR THRESHOLD(20,1)|STIRRING TEMPERATURE(19,2)|NUTSHELL ACTIVATED CARBON(18,1)|NITROGEN ATMOSPHERE(17,8)|P THIOCRESOL MOLAR RATIO(17,8)|PHOTOCHEMICAL REACTION(17,1)|ODOR(15,12)|ACTIVE CARBON POWDER(15,2)|FIXED BED REACTOR(14,8)|MERCAPTO FUNCTIONAL GROUP(14,2)|REACTION ATMOSPHERE(14,2)|THIOUREA MOLAR RATIO(13,7)|DRYING CONDITION(13,2)|STIRRING CONDITION(13,2)|COMPLEX OPERATION MANAGEMENT(13,1)|OXIDATION REACTION(13,1)|AMMONIA INTRODUCTION(12,6)|SULFYDRYL PREPOLYMERIZATION MASS RATIO(12,6)|ACID RAIN(12,1)|HEAT TREATMENT(11,11)|ACTIVE CARBON MODIFICATION(11,2)|PITCH ACTIVATED CARBON(11,2)|DIRECT PROPORTION(11,1)|VOLUME RATIO(10,4)|DRYING TEMPERATURE(10,2)|REACTION TEMPERATURE(9,9)|MEDICINE STORAGE DEVICE(9,1)|RAW COAL ACTIVATED CARBON(8,5)|ADSORPTION TOWER(8,2)|ODOR POLLUTION(8,2)|THIOL PREPOLYMERIZATION MODIFICATION SOLUTION(8,2)|DIGESTIVE SYSTEM(8,1)|FRUIT ADSORPTION(8,1)|MASS RATIO(7,16)|SOLUTION DILUTION(7,6)|AIRSPEED(7,5)|THIOUREA FORMALDEHYDE RESIN(7,2)|ENDOCRINE SYSTEM(7,1)|LIQUID MEDICINE STORAGE DEVICE(7,1)|NERVOUS SYSTEM(7,1)|SYNTHETIC RESIN(6,6)|STIRRING TIME(6,4)|ACIDIC SUBSTANCE(6,2)|DILUENT ADDITION VOLUME ML(6,2)|HUMAN BODY(6,2)|OPERATION COST(6,2)|REACTION VESSEL(6,2)|RESPIRATORY SYSTEM(6,2)|MALODOR MANAGEMENT(6,1)|PEOPLE SMELL(6,1)|SULFYDRYL DISTRIBUTION(6,1)|DEIONIZED WATER(5,25)|AMINO GROUP(5,4)|ASPHALT ACTIVATED CARBON(5,3)|ALKALINE CAUSTIC SODA(5,1)|AMMONIA ALDEHYDE(5,1)|AMMONIA PHENOL(5,1)|AQUEOUS FORMALDEHYDE(5,1)|CARRYING OUT MODIFICATION TREATMENT(5,1)|CONTROLLABLE MERCAPTO GROUP(5,1)|ION DIPOLE BOND(5,1)|LIVING ENVIRONMENT QUALITY(5,1)|MALODOROUS GAS PURIFICATION TREATMENT(5,1)|MALODOROUS REMOVAL(5,1)|MERCAPTO POLYMERIZATION MODIFICATION SOLUTION(5,1)|PEOPLE REQUIREMENT(5,1)|PUBLIC HAZARD(5,1)|SULFYDRYL CONTENT(5,1)|OPEN CONTAINER(4,8)|HEAT TREATMENT TEMPERATURE(4,3)|AMINO ALDEHYDE GROUP(4,2)|DRYING TIME(4,2)|PARTICLE SIZE(4,2)||(CN109967036)|ACTIVATED CARBON MODIFICATION(100,49)|SULFYDRYL MODIFIED ACTIVATED CARBON(100,24)|MALODOR REMOVAL(100,5)|SULFYDRYL PREPOLYMERIZATION MODIFICATION(100,1)|SULFYDRYL PREPOLYMERIZATION(85,33)|MERCAPTOMODIFIED ACTIVATED CARBON(66,15)|MERCAPTO PREPOLYMERIZATION MODIFICATION SOLUTION(47,2)|FORMALDEHYDE(41,47)|SULFHYDRYL PREPOLYMERIZATION MODIFICATION SOLUTION(40,4)|SULFHYDRYL MODIFIED ACTIVATED CARBON(35,3)|MIXING P THIOCRESOL(29,11)|ACTIVATED CARBON(28,58)|THIOUREA(28,17)|MERCAPTOGROUP PREPOLYMERIZATION MASS RATIO(28,1)|ACTIVATED CARBON POWDER(27,31)|ADJUSTABLE MERCAPTO GROUP(24,1)|TOTAL PREPOLYMER SOLUTION(23,25)|SATURATED ADSORPTION CAPACITY(21,12)|ABRASIVE(21,9)|ABSOLUTE ALCOHOL(20,2)|MIXING THIOUREA(20,2)|STIRRING TEMPERATURE(19,2)|NUTSHELL ACTIVATED CARBON(18,1)|NITROGEN ATMOSPHERE(17,8)|ABRASIVE CONDITION(15,2)|ACTIVE CARBON POWDER(15,2)|FIXED BED REACTOR(14,8)|REACTION ATMOSPHERE(14,2)|P THIOCRESOL MOLAR RATIO(13,8)|THIOUREA MOLAR RATIO(13,7)|ABRASIVE TEMPERATURE(13,2)|STIRRING CONDITION(13,2)|AMMONIA INTRODUCTION(12,6)|SULFYDRYL PREPOLYMERIZATION MASS RATIO(12,6)|HEAT TREATMENT(11,11)|ACTIVE CARBON MODIFICATION(11,2)|PITCH ACTIVATED CARBON(11,2)|SUBSTANCE AMMONIA COMPOUNDSTHE(10,1)|REACTION TEMPERATURE(9,9)|RAW COAL ACTIVATED CARBON(8,5)|ADSORPTION TOWER(8,2)|ODOR POLLUTION(8,2)|THIOL PREPOLYMERIZATION MODIFICATION SOLUTION(8,2)|FRUIT ADSORPTION(8,1)|SOLUTION DILUTION(7,6)|DEODORIZATION(7,4)|THIOUREA FORMALDEHYDE RESIN(7,2)|SYNTHETIC RESIN(6,6)|AIRSPEED(6,4)|STIRRING TIME(6,4)|VOLUME RATIO(6,4)|ACIDIC SUBSTANCE(6,2)|DILUENT ADDITION VOLUME ML(6,2)|REACTION VESSEL(6,2)|MALODOR MANAGEMENT(6,1)|MALODOROUS SUBSTANCE(6,1)|PEOPLE SMELL(6,1)|DEIONIZED WATER(5,25)|AMINO GROUP(5,4)|ASPHALT ACTIVATED CARBON(5,3)|ABRASIVE TIME(5,2)|ALKALINE CAUSTIC SODA(5,1)|AMMONIA ALDEHYDE(5,1)|AMMONIA PHENOL(5,1)|AQUEOUS FORMALDEHYDE(5,1)|CARRYING OUT MODIFICATION TREATMENT(5,1)|CONTROLLABLE MERCAPTO GROUP(5,1)|ION DIPOLE BOND(5,1)|LIVING ENVIRONMENT QUALITY(5,1)|MALODOROUS GAS PURIFICATION TREATMENT(5,1)|MALODOROUS REMOVAL(5,1)|PEOPLE REQUIREMENT(5,1)|PUBLIC HAZARD(5,1)|OPEN CONTAINER(4,8)|HEAT TREATMENT TEMPERATURE(4,3)|AMINO ALDEHYDE GROUP(4,2)|PARTICLE SIZE(4,2)|ALKALINE SUBSTANCE(4,1)|CARBONIZATION TEMPERATURE(4,1)|NEUTRAL SUBSTANCE(4,1)|PENETRATION CAPACITY(4,1)|RAW BIOMASS ACTIVATED CARBON(4,1)| (CN109967036)|1. A preparation method of sulfydryl modified activated carbon comprises the following steps:|1) crushing the activated carbon to prepare activated carbon powder;|2) mixing p-methyl thiophenol, thiourea, formaldehyde and water, heating and stirring to prepare a sulfydryl prepolymerization modified solution;|3) modifying the active carbon powder prepared in the step 1) by using the sulfhydryl prepolymerization modification solution prepared in the step 2) to prepare modified active carbon;|4) drying the modified activated carbon prepared in the step 3), and then carrying out heat treatment to obtain the required sulfydryl modified activated carbon;|in the step 2), the preparation process of the sulfhydryl prepolymerization modification solution comprises the following steps:|A) mixing p-methyl thiophenol, formaldehyde and water, and heating and stirring to obtain a first prepolymer solution;|B) mixing thiourea, formaldehyde and water, and heating and stirring to prepare a second prepolymer solution;|C) cooling and mixing the first prepolymer solution prepared in the step A) and the second prepolymer solution prepared in the step B) to obtain a total prepolymer solution, and diluting the total prepolymer solution with water to obtain a sulfhydryl prepolymerization modified solution;|the preparation process of the mercapto prepolymerization modification liquid comprises any one or more of the following conditions:|A1) in the step A), the molar ratio of p-methylthiophenol to formaldehyde is 1: 1.5-2.5;|A2) in the step A), the volume ratio of the water to the formaldehyde is 1-10: 1-2;|A3) in the step B), the molar ratio of the thiourea to the formaldehyde is 1: 1.5-2.5;|A4) in the step B), the volume ratio of the water to the formaldehyde is 1-10: 1-2;|A5) in the step C), the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.2-0.8: 1.|2. The method for producing a mercapto-modified activated carbon according to claim 1, wherein in step 1), the activated carbon is selected from one of wood-based activated carbon, nutshell activated carbon, coal-based activated carbon, pitch-based activated carbon, and synthetic resin-based activated carbon; the particle size of the activated carbon powder is 200-600 meshes.|3. The method of producing a mercapto-modified activated carbon according to claim 1, characterized by comprising any one or more of the following conditions:|A1) in the step A), the heating and stirring temperature is 65-75 ℃, and the heating and stirring time is 0.5-4 h;|A2) in the step B), the heating and stirring temperature is 35-45 ℃, and the heating and stirring time is 0.5-4 h.|4. The method for preparing mercapto-modified activated carbon according to claim 1, wherein in step 3), the modification treatment is carried out by immersing activated carbon powder in a mercapto prepolymerization modification solution, adding a diluent, and heating and stirring until the solution is completely evaporated to obtain the modified activated carbon.|5. The method for preparing mercapto-modified activated carbon according to claim 4, wherein in step 3), any one or more of the following conditions are included:|B1) the mass ratio of the mercapto-group prepolymerization modified solution to the activated carbon powder is 1-30: 100;|B2) the diluent is selected from one of water or absolute ethyl alcohol;|B3) the ratio of the addition volume mL of the diluent to the addition mass g of the activated carbon powder is 0-10 mL/g;|B4) the heating and stirring conditions are as follows: a reaction vessel: an open container; reaction temperature: 70-90 ℃.|6. The method for preparing mercapto-modified activated carbon according to claim 1, wherein in step 4), any one or more of the following conditions are included:|C1) the drying conditions are as follows: drying temperature: 80-110 ℃; drying time: 6-48 h;|C2) the conditions of the heat treatment are as follows: reaction atmosphere: a nitrogen atmosphere; the heat treatment temperature is as follows: 350-600 ℃; and (3) heat treatment time: 2-6 h.|7. A mercapto-modified activated carbon prepared by the method of preparing a mercapto-modified activated carbon according to any one of claims 1 to 6.|8. Use of the mercapto-modified activated carbon according to claim 7 in purification treatment of ammonia-containing malodorous gases.|9. The use according to claim 8, wherein the mercapto-modified activated carbon is packed in a fixed bed reactor, and malodorous gas containing ammonia is introduced. (CN109967036)|TECHNICAL FIELD|[0002] The invention belongs to the technical field of environmental pollution treatment, relates to a preparation method of sulfhydryl modified activated carbon for removing malodor, and particularly relates to a preparation method of activated carbon with adjustable content of sulfhydryl functional groups for removing malodor.|BACKGROUND ART|[0004] The stink acts on the smell of people and causes harm to people, and is one of seven typical public hazards in the world. The malodorous pollutants not only cause adverse psychological effects to people, but also cause damages to the respiratory system, the digestive system, the cardiovascular and cerebrovascular systems, the endocrine system and the nervous system of human bodies to different degrees, and some malodorous pollutants can also generate oxidation reaction and photochemical reaction in troposphere atmosphere, thereby playing an important role in acid rain and photochemical smog pollution. With the rapid development of the urbanization process, the requirements of people on the quality of the living environment are increasingly improved, and the influence of malodorous substances on urban living areas is more and more remarkable and is paid more and more attention. As early as 50-60 years of the 20 th century, the problem of odor pollution appears in developed countries, and complaints about odor pollution are increased, but the complaints about odor in various large and medium-sized cities in China are also increased gradually and are used as a form of air pollution, and malodorous gas takes air as a transmission medium and affects human bodies through a respiratory system. Because the odor threshold of the malodorous substances is low, the sensory quantity (odor intensity) of people is in direct proportion to the logarithm of the stimulation quantity of the human olfactory sensation, the components are complex and have the characteristics of time interval, regionality and seasonality, the pollution events are increased day by day, and the treatment and management difficulty is increased more and more.|[0005] Common methods for malodour management are water washing and chemical deodorization. The water cleaning method is characterized in that ammonia gas and hydrogen sulfide gas in the odor are contacted and dissolved with water by utilizing the characteristic that certain substances in the odor can be dissolved in water, so that the aim of deodorization is fulfilled. The chemical deodorization method utilizes the characteristics of neutralization reaction between some substances in the odor and the liquid medicine, such as removing acidic substances such as hydrogen sulfide in the odor by using alkaline caustic soda and sodium hypochlorite solution, and removing alkaline substances such as ammonia in the odor by using acidic solution such as hydrochloric acid. Compared with the activated carbon adsorption method, the chemical deodorization method needs to be provided with more auxiliary facilities such as a liquid medicine storage device, a liquid medicine conveying device, a discharging device and the like, has more complex operation management and higher operation cost, and has lower efficiency because the odor which does not react with the liquid medicine is difficult to remove.|[0006] The active carbon adsorption method is to utilize the characteristic that active carbon can adsorb odor-causing substances in odor to achieve the aim of deodorization. In order to effectively deodorize, various kinds of activated carbon having different properties are generally used, and an activated carbon for adsorbing an acidic substance, an activated carbon for adsorbing a basic substance and an activated carbon for adsorbing a neutral substance are installed in an adsorption tower, and after the odor is brought into contact with the various kinds of activated carbons, the odor is discharged out of the adsorption tower. Compared with water cleaning and liquid cleaning methods, the method has higher efficiency, but the activated carbon is saturated when being adsorbed to a certain amount, and the activated carbon needs to be regenerated or replaced, so the operation cost is higher. Therefore, the key point of the active carbon adsorption method for treating the odor is to modify the active carbon to improve the adsorption efficiency of the active carbon.|DISCLOSURE|[0007] Disclosure of Invention|[0008] In view of the above-mentioned shortcomings of the prior art, the present invention aims to provide a method for preparing a mercapto activated carbon with uniform distribution of mercapto groups and adjustable content of mercapto functional groups, so as to solve the problem of lack of an activated carbon with high efficiency for removing malodors in the prior art.|[0009] To achieve the above and other related objects, there is provided, in a first aspect of the present invention, a method for preparing mercapto-modified activated carbon for removing malodor, comprising the steps of:|[0010] 1) crushing the activated carbon to prepare activated carbon powder;|[0011] 2) mixing p-methyl thiophenol, thiourea, formaldehyde and water, heating and stirring to prepare a sulfydryl prepolymerization modified solution;|[0012] 3) modifying the active carbon powder prepared in the step 1) by using the sulfhydryl prepolymerization modification solution prepared in the step 2) to prepare modified active carbon;|[0013] 4) drying the modified activated carbon prepared in the step 3), and then carrying out heat treatment to obtain the required sulfydryl modified activated carbon.|[0014] Preferably, in step 1), the activated carbon is selected from one of wood activated carbon, nut shell activated carbon, coal activated carbon, pitch-based activated carbon, or synthetic resin-based activated carbon.|[0015] Preferably, in the step 1), the particle size of the activated carbon powder is 200-600 meshes.|[0016] Preferably, in step 2), the water is deionized water.|[0017] Preferably, in the step 2), the preparation process of the thiol prepolymerization modification solution comprises the following steps:|[0018] A) mixing p-methyl thiophenol, formaldehyde and water, and heating and stirring to obtain a first prepolymer solution;|[0019] B) mixing thiourea, formaldehyde and water, and heating and stirring to prepare a second prepolymer solution;|[0020] C) cooling and mixing the first prepolymer solution prepared in the step A) and the second prepolymer solution prepared in the step B) to obtain a total prepolymer solution, and diluting the total prepolymer solution with water to obtain the sulfhydryl prepolymerization modified solution.|[0021] More preferably, in the step A), the mol ratio of the p-methylthiophenol to the formaldehyde is 1: 1.5-2.5. Further preferably, the molar ratio of p-methylthiophenol to formaldehyde added is 1: 2.|[0022] More preferably, in step a), the volume ratio of water to formaldehyde added is from 1 to 10: 1-2.|[0023] More preferably, in step A), the temperature of the heating and stirring is 65-75 ℃. Further preferably, the temperature of the heating and stirring is 70 ℃.|[0024] More preferably, in the step A), the heating and stirring time is 0.5-4 h.|[0025] More preferably, in the step B), the molar ratio of the thiourea to the formaldehyde is 1: 1.5-2.5. Further preferably, the molar ratio of thiourea to formaldehyde addition is 1: 2.|[0026] More preferably, in step B), the volume ratio of water to formaldehyde added is from 1 to 10: 1-2.|[0027] More preferably, in step B), the temperature of the heating and stirring is 35-45 ℃. Further preferably, the temperature of the heating and stirring is 40 ℃.|[0028] More preferably, in the step B), the heating and stirring time is 0.5-4 h.|[0029] More preferably, in step a) or B), the formaldehyde is an aqueous formaldehyde solution having a concentration of 37 wt% by mass.|[0030] More preferably, in step C), the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.2-0.8: 1.|[0031] More preferably, in the step C), the concentration of the sulfhydryl prepolymerization modification solution is 100-200 g/L.|[0032] Preferably, in the step 3), the modification treatment is to soak the activated carbon powder in the thiol prepolymerization modification solution, add a diluent, and heat and stir until the solution is completely evaporated, so as to obtain the modified activated carbon.|[0033] More preferably, the mass ratio of the sulfhydryl prepolymerization modification solution to the activated carbon powder is 1-30: 100.|[0034] More preferably, the diluent is selected from one of water or absolute ethanol. The water is deionized water. The diluent can ensure that the activated carbon powder can be completely immersed in the diluent solution.|[0035] More preferably, the ratio of the addition volume mL of the diluent to the addition mass g of the activated carbon powder is 0-10 mL/g.|[0036] More preferably, the heating and stirring conditions are as follows: a reaction vessel: an open container; reaction temperature: 70-90 ℃.|[0037] Preferably, in step 4), the drying conditions are as follows: drying temperature: 80-110 ℃; drying time: 6-48 h.|[0038] Preferably, in step 4), the heat treatment conditions are as follows: reaction atmosphere: a nitrogen atmosphere; the heat treatment temperature is as follows: 350-600 ℃; and (3) heat treatment time: 2-6 h.|[0039] The invention provides sulfydryl modified activated carbon, which is prepared by the method.|[0040] The third aspect of the invention provides the application of the sulfhydryl modified activated carbon in the purification treatment of ammonia-containing malodorous gas.|[0041] Preferably, the ammonia-containing component in the ammonia-containing malodorous gas is one or more of ammonia-containing amino group, ammonia aldehyde group, ammonia hydroxyl group, ammonia carboxyl group or ammonia phenol-containing component.|[0042] Preferably, the application is to fill the mercapto-modified activated carbon into a fixed bed reactor and introduce ammonia-containing malodorous gas.|[0043] More preferably, the reaction temperature is 20-80 ℃.|[0044] More preferably, the malodorous gas may be operated at a pressure of 0.1 to 10 MPa.|[0045] More preferably, the space velocity of the malodorous gas is 500-20000 h-1。|[0046] More preferably, the concentration of the ammonia-containing compound in the malodorous gas is 10-3000 ppm.|[0047] As described above, the present invention provides a method for preparing a mercapto-modified activated carbon for removing malodor, which initially modifies and heat-treats activated carbon with a mercapto polymerization modification solution comprising p-methylthiophenol, thiourea and formaldehyde, thereby fixing a carbonized film containing mercapto groups on the surface of activated carbon to prepare the mercapto-modified activated carbon. Has the following beneficial effects:|[0048] (1) the method can uniformly coat p-methylthiophenol-thiourea-formaldehyde resin on the surface of the activated carbon, can regulate and control the content of the sulfydryl functional group in a larger range by regulating the ratio of the p-methylthiophenol to the activated carbon, and finally obtains the sulfydryl modified activated carbon with uniformly distributed and regulated sulfydryl through heat treatment. Therefore, the technical problems that in the prior art, the active molecules containing sulfydryl react with a certain specific functional group (such as hydroxyl) on the surface of the active carbon to fix the sulfydryl on the surface of the active carbon, the distribution of the sulfydryl is not uniform, and the content of the sulfydryl cannot be regulated and controlled are solved.|[0049] (2) The urea-formaldehyde resin synthesized by thiourea-formaldehyde resin is taken as a matrix, so that on one hand, the heat treatment temperature of the surface resin can be reduced due to the lower carbonization temperature, and the mercapto functional group can be furthest stored; on the other hand, a large number of sulfur-containing functional groups with higher alkalinity are introduced to the surface of the activated carbon, and cations of the functional groups can directly accept electrons from malodor molecules to form ion dipole bonds, so that the malodor removal efficiency of the modified activated carbon is further enhanced.|[0050] (3) The mercapto modified activated carbon prepared by the preparation method has uniform surface mercapto distribution and adjustable mercapto functional group content, shows extremely high adsorption efficiency, penetration capacity and circulation efficiency when used for adsorbing malodorous gas, and is extremely suitable for purifying malodorous gas containing amino groups, amino aldehyde groups, amino hydroxyl groups, amino carboxyl groups or amino phenol components.|INVENTION MODE|[0051] Detailed Description|[0052] The present invention is further illustrated below with reference to specific examples, which are intended to be illustrative only and not to limit the scope of the invention.|[0053] The embodiments of the present invention are described below with reference to specific embodiments, and other advantages and effects of the present invention will be easily understood by those skilled in the art from the disclosure of the present specification. The invention is capable of other and different embodiments and of being practiced or of being carried out in various ways, and its several details are capable of modification in various respects, all without departing from the spirit and scope of the present invention.|[0054] Example 1|[0055] Weighing 100g of wood activated carbon, and crushing the wood activated carbon into activated carbon powder of 200-300 meshes.|[0056] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 0.5h to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) with corresponding mass according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 0.5h to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.2, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 100g/L to obtain the sulfhydryl prepolymerization modified solution.|[0057] Weighing 10mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 1:100, and adding a proper amount of absolute ethyl alcohol as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at 70 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0058] And finally, drying the modified activated carbon at 80 ℃ for 6h, and then carrying out heat treatment at 350 ℃ for 2h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0059] Respectively filling raw wood activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 20 ℃, introducing ammonia-containing gas, controlling the pressure at 0.1MPa, controlling the concentration of an ammonia-containing compound at 10ppm, and controlling the airspeed at 500h-1The adsorption efficiency of the raw biomass activated carbon is 80 percent, the saturated adsorption capacity is 167mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 90 percent, and the saturated adsorption capacity is 213 mg/g.|[0060] Example 2|[0061] Weighing 100g of the shell activated carbon, and crushing the shell activated carbon into activated carbon powder of 200-300 meshes.|[0062] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 4 hours to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 4 hours to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.8, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 200g/L to obtain the sulfhydryl prepolymerization modified solution.|[0063] Weighing 150mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 30:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at the temperature of 90 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0064] And finally, drying the modified activated carbon at 110 ℃ for 48h, and then carrying out heat treatment at 600 ℃ for 6h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0065] Respectively filling raw fruit shell activated carbon and the sulfydryl modified activated carbon into a fixed bed reactor, controlling the reaction temperature at 80 ℃, introducing ammonia-containing gas, controlling the pressure at 10MPa, controlling the concentration of ammonia-containing compounds at 3000ppm, and controlling the airspeed at 20000h-1The adsorption efficiency of the original fruit shell activated carbon is 55 percent, the saturated adsorption capacity is 120mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 79 percent, and the saturated adsorption capacity is 209 mg/g.|[0066] Example 3|[0067] 100g of coal-based activated carbon is weighed and crushed into activated carbon powder of 300-400 meshes.|[0068] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 1 hour to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 3 hours to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.5, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 150g/L to obtain the sulfhydryl prepolymerization modified solution.|[0069] Weighing 66.7mL of sulfydryl pre-polymerization modified solution, placing the sulfydryl pre-polymerization modified solution in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified solution, wherein the mass ratio of the sulfydryl pre-polymerization modified solution to the activated carbon powder is 10:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at 80 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0070] And finally, drying the modified activated carbon at 100 ℃ for 36h, and then carrying out heat treatment at 500 ℃ for 4h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0071] Respectively filling raw coal activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 38 ℃, introducing ammonia-containing gas, controlling the pressure at 0.5MPa, controlling the concentration of ammonia-containing compounds at 100ppm, and controlling the airspeed at 6000h-1The adsorption efficiency of the raw coal-based activated carbon is 83 percent, the saturated adsorption capacity is 312mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 97 percent, and the saturated adsorption capacity is 423 mg/g.|[0072] Example 4|[0073] Weighing 100g of asphalt-based activated carbon, and crushing the asphalt-based activated carbon to 400-600 meshes of activated carbon powder.|[0074] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 2.5 hours to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) with corresponding mass according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 1.8h to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.4, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 100g/L to obtain the sulfhydryl prepolymerization modified solution.|[0075] Weighing 200mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 20:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at 85 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0076] And finally, drying the modified activated carbon at 90 ℃ for 24h, and then carrying out heat treatment at 400 ℃ for 3h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0077] Respectively filling the original asphalt-based activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 60 ℃, introducing ammonia-containing gas, controlling the pressure at 5MPa, controlling the concentration of an ammonia-containing compound at 1000ppm, and controlling the airspeed at 12000h-1The adsorption efficiency of the raw coal-based activated carbon is 85 percent, the saturated adsorption capacity is 267mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 98 percent, and the saturated adsorption capacity is 369 mg/g.|[0078] Example 5|[0079] 100g of synthetic resin-based activated carbon is weighed and crushed into activated carbon powder of 200-600 meshes.|[0080] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 2 hours to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) with corresponding mass according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 3.6h to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.7, and finally diluting the total prepolymer solution by using deionized water until the concentration of the total prepolymer solution is 120g/L to obtain the sulfhydryl prepolymerization modified solution.|[0081] Weighing 208mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 25:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at 80 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0082] And finally, drying the modified activated carbon at 95 ℃ for 38h, and then carrying out heat treatment at 450 ℃ for 3h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0083] Respectively filling the original synthetic resin-based activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 25 ℃, introducing ammonia-containing gas, controlling the pressure at 8MPa, controlling the concentration of ammonia-containing compounds at 700ppm and the space velocity at 9000h-1The adsorption efficiency of the raw coal-based activated carbon is 76%, the saturated adsorption capacity is 200mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 99%, and the saturated adsorption capacity is 397 mg/g.|[0084] Example 6|[0085] 100g of synthetic resin-based activated carbon is weighed and crushed into activated carbon powder of 200-600 meshes.|[0086] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 3.5 hours to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 1h to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.3, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 180g/L to obtain the sulfhydryl prepolymerization modified solution.|[0087] Weighing 83mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 15:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at the temperature of 90 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0088] And finally, drying the modified activated carbon at 105 ℃ for 14h, and then carrying out heat treatment at 580 ℃ for 3h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0089] Respectively filling the original synthetic resin-based activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 30 ℃, introducing ammonia-containing gas, controlling the pressure at 0.6MPa, controlling the concentration of an ammonia-containing compound at 1500ppm, and controlling the airspeed at 5000h-1The adsorption efficiency of the raw coal-based activated carbon is 73 percent, the saturated adsorption capacity is 198mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 94 percent, and the saturated adsorption capacity is 302 mg/g.|[0090] In summary, the preparation method of the mercapto-modified activated carbon for removing malodorous gas provided by the invention can obtain the mercapto-modified activated carbon with uniformly distributed and controllable mercapto groups, further enhance the malodorous removal efficiency of the modified activated carbon, and is suitable for purification treatment of malodorous gas containing amino groups, amino aldehyde groups, amino hydroxyl groups, amino carboxyl groups or amino phenol components. Therefore, the invention effectively overcomes various defects in the prior art and has high industrial utilization value.|[0091] The foregoing embodiments are merely illustrative of the principles and utilities of the present invention and are not intended to limit the invention. Any person skilled in the art can modify or change the above-mentioned embodiments without departing from the spirit and scope of the present invention. Accordingly, it is intended that all equivalent modifications or changes which can be made by those skilled in the art without departing from the spirit and technical spirit of the present invention be covered by the claims of the present invention. (CN109967036)|TECHNICAL FIELD|[0002] The invention belongs to the technical field of environmental pollution treatment, relates to a preparation method of sulfhydryl modified activated carbon for removing malodor, and particularly relates to a preparation method of activated carbon with adjustable content of sulfhydryl functional groups for removing malodor.|BACKGROUND ART|[0004] The stink acts on the smell of people and causes harm to people, and is one of seven typical public hazards in the world. The malodorous pollutants not only cause adverse psychological effects to people, but also cause damages to the respiratory system, the digestive system, the cardiovascular and cerebrovascular systems, the endocrine system and the nervous system of human bodies to different degrees, and some malodorous pollutants can also generate oxidation reaction and photochemical reaction in troposphere atmosphere, thereby playing an important role in acid rain and photochemical smog pollution. With the rapid development of the urbanization process, the requirements of people on the quality of the living environment are increasingly improved, and the influence of malodorous substances on urban living areas is more and more remarkable and is paid more and more attention. As early as 50-60 years of the 20 th century, the problem of odor pollution appears in developed countries, and complaints about odor pollution are increased, but the complaints about odor in various large and medium-sized cities in China are also increased gradually and are used as a form of air pollution, and malodorous gas takes air as a transmission medium and affects human bodies through a respiratory system. Because the odor threshold of the malodorous substances is low, the sensory quantity (odor intensity) of people is in direct proportion to the logarithm of the stimulation quantity of the human olfactory sensation, the components are complex and have the characteristics of time interval, regionality and seasonality, the pollution events are increased day by day, and the treatment and management difficulty is increased more and more.|[0005] Common methods for malodour management are water washing and chemical deodorization. The water cleaning method is characterized in that ammonia gas and hydrogen sulfide gas in the odor are contacted and dissolved with water by utilizing the characteristic that certain substances in the odor can be dissolved in water, so that the aim of deodorization is fulfilled. The chemical deodorization method utilizes the characteristics of neutralization reaction between some substances in the odor and the liquid medicine, such as removing acidic substances such as hydrogen sulfide in the odor by using alkaline caustic soda and sodium hypochlorite solution, and removing alkaline substances such as ammonia in the odor by using acidic solution such as hydrochloric acid. Compared with the activated carbon adsorption method, the chemical deodorization method needs to be provided with more auxiliary facilities such as a liquid medicine storage device, a liquid medicine conveying device, a discharging device and the like, has more complex operation management and higher operation cost, and has lower efficiency because the odor which does not react with the liquid medicine is difficult to remove.|[0006] The active carbon adsorption method is to utilize the characteristic that active carbon can adsorb odor-causing substances in odor to achieve the aim of deodorization. In order to effectively deodorize, various kinds of activated carbon having different properties are generally used, and an activated carbon for adsorbing an acidic substance, an activated carbon for adsorbing a basic substance and an activated carbon for adsorbing a neutral substance are installed in an adsorption tower, and after the odor is brought into contact with the various kinds of activated carbons, the odor is discharged out of the adsorption tower. Compared with water cleaning and liquid cleaning methods, the method has higher efficiency, but the activated carbon is saturated when being adsorbed to a certain amount, and the activated carbon needs to be regenerated or replaced, so the operation cost is higher. Therefore, the key point of the active carbon adsorption method for treating the odor is to modify the active carbon to improve the adsorption efficiency of the active carbon.|DISCLOSURE|[0007] Disclosure of Invention|[0008] In view of the above-mentioned shortcomings of the prior art, the present invention aims to provide a method for preparing a mercapto activated carbon with uniform distribution of mercapto groups and adjustable content of mercapto functional groups, so as to solve the problem of lack of an activated carbon with high efficiency for removing malodors in the prior art.|[0009] To achieve the above and other related objects, there is provided, in a first aspect of the present invention, a method for preparing mercapto-modified activated carbon for removing malodor, comprising the steps of:|[0010] 1) crushing the activated carbon to prepare activated carbon powder;|[0011] 2) mixing p-methyl thiophenol, thiourea, formaldehyde and water, heating and stirring to prepare a sulfydryl prepolymerization modified solution;|[0012] 3) modifying the active carbon powder prepared in the step 1) by using the sulfhydryl prepolymerization modification solution prepared in the step 2) to prepare modified active carbon;|[0013] 4) drying the modified activated carbon prepared in the step 3), and then carrying out heat treatment to obtain the required sulfydryl modified activated carbon.|[0014] Preferably, in step 1), the activated carbon is selected from one of wood activated carbon, nut shell activated carbon, coal activated carbon, pitch-based activated carbon, or synthetic resin-based activated carbon.|[0015] Preferably, in the step 1), the particle size of the activated carbon powder is 200-600 meshes.|[0016] Preferably, in step 2), the water is deionized water.|[0017] Preferably, in the step 2), the preparation process of the thiol prepolymerization modification solution comprises the following steps:|[0018] A) mixing p-methyl thiophenol, formaldehyde and water, and heating and stirring to obtain a first prepolymer solution;|[0019] B) mixing thiourea, formaldehyde and water, and heating and stirring to prepare a second prepolymer solution;|[0020] C) cooling and mixing the first prepolymer solution prepared in the step A) and the second prepolymer solution prepared in the step B) to obtain a total prepolymer solution, and diluting the total prepolymer solution with water to obtain the sulfhydryl prepolymerization modified solution.|[0021] More preferably, in the step A), the mol ratio of the p-methylthiophenol to the formaldehyde is 1: 1.5-2.5. Further preferably, the molar ratio of p-methylthiophenol to formaldehyde added is 1: 2.|[0022] More preferably, in step a), the volume ratio of water to formaldehyde added is from 1 to 10: 1-2.|[0023] More preferably, in step A), the temperature of the heating and stirring is 65-75 ℃. Further preferably, the temperature of the heating and stirring is 70 ℃.|[0024] More preferably, in the step A), the heating and stirring time is 0.5-4 h.|[0025] More preferably, in the step B), the molar ratio of the thiourea to the formaldehyde is 1: 1.5-2.5. Further preferably, the molar ratio of thiourea to formaldehyde addition is 1: 2.|[0026] More preferably, in step B), the volume ratio of water to formaldehyde added is from 1 to 10: 1-2.|[0027] More preferably, in step B), the temperature of the heating and stirring is 35-45 ℃. Further preferably, the temperature of the heating and stirring is 40 ℃.|[0028] More preferably, in the step B), the heating and stirring time is 0.5-4 h.|[0029] More preferably, in step a) or B), the formaldehyde is an aqueous formaldehyde solution having a concentration of 37 wt% by mass.|[0030] More preferably, in step C), the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.2-0.8: 1.|[0031] More preferably, in the step C), the concentration of the sulfhydryl prepolymerization modification solution is 100-200 g/L.|[0032] Preferably, in the step 3), the modification treatment is to soak the activated carbon powder in the thiol prepolymerization modification solution, add a diluent, and heat and stir until the solution is completely evaporated, so as to obtain the modified activated carbon.|[0033] More preferably, the mass ratio of the sulfhydryl prepolymerization modification solution to the activated carbon powder is 1-30: 100.|[0034] More preferably, the diluent is selected from one of water or absolute ethanol. The water is deionized water. The diluent can ensure that the activated carbon powder can be completely immersed in the diluent solution.|[0035] More preferably, the ratio of the addition volume mL of the diluent to the addition mass g of the activated carbon powder is 0-10 mL/g.|[0036] More preferably, the heating and stirring conditions are as follows: a reaction vessel: an open container; reaction temperature: 70-90 ℃.|[0037] Preferably, in step 4), the drying conditions are as follows: drying temperature: 80-110 ℃; drying time: 6-48 h.|[0038] Preferably, in step 4), the heat treatment conditions are as follows: reaction atmosphere: a nitrogen atmosphere; the heat treatment temperature is as follows: 350-600 ℃; and (3) heat treatment time: 2-6 h.|[0039] The invention provides sulfydryl modified activated carbon, which is prepared by the method.|[0040] The third aspect of the invention provides the application of the sulfhydryl modified activated carbon in the purification treatment of ammonia-containing malodorous gas.|[0041] Preferably, the ammonia-containing component in the ammonia-containing malodorous gas is one or more of ammonia-containing amino group, ammonia aldehyde group, ammonia hydroxyl group, ammonia carboxyl group or ammonia phenol-containing component.|[0042] Preferably, the application is to fill the mercapto-modified activated carbon into a fixed bed reactor and introduce ammonia-containing malodorous gas.|[0043] More preferably, the reaction temperature is 20-80 ℃.|[0044] More preferably, the malodorous gas may be operated at a pressure of 0.1 to 10 MPa.|[0045] More preferably, the space velocity of the malodorous gas is 500-20000 h-1。|[0046] More preferably, the concentration of the ammonia-containing compound in the malodorous gas is 10-3000 ppm.|[0047] As described above, the present invention provides a method for preparing a mercapto-modified activated carbon for removing malodor, which initially modifies and heat-treats activated carbon with a mercapto polymerization modification solution comprising p-methylthiophenol, thiourea and formaldehyde, thereby fixing a carbonized film containing mercapto groups on the surface of activated carbon to prepare the mercapto-modified activated carbon. Has the following beneficial effects:|[0048] (1) the method can uniformly coat p-methylthiophenol-thiourea-formaldehyde resin on the surface of the activated carbon, can regulate and control the content of the sulfydryl functional group in a larger range by regulating the ratio of the p-methylthiophenol to the activated carbon, and finally obtains the sulfydryl modified activated carbon with uniformly distributed and regulated sulfydryl through heat treatment. Therefore, the technical problems that in the prior art, the active molecules containing sulfydryl react with a certain specific functional group (such as hydroxyl) on the surface of the active carbon to fix the sulfydryl on the surface of the active carbon, the distribution of the sulfydryl is not uniform, and the content of the sulfydryl cannot be regulated and controlled are solved.|[0049] (2) The urea-formaldehyde resin synthesized by thiourea-formaldehyde resin is taken as a matrix, so that on one hand, the heat treatment temperature of the surface resin can be reduced due to the lower carbonization temperature, and the mercapto functional group can be furthest stored; on the other hand, a large number of sulfur-containing functional groups with higher alkalinity are introduced to the surface of the activated carbon, and cations of the functional groups can directly accept electrons from malodor molecules to form ion dipole bonds, so that the malodor removal efficiency of the modified activated carbon is further enhanced.|[0050] (3) The mercapto modified activated carbon prepared by the preparation method has uniform surface mercapto distribution and adjustable mercapto functional group content, shows extremely high adsorption efficiency, penetration capacity and circulation efficiency when used for adsorbing malodorous gas, and is extremely suitable for purifying malodorous gas containing amino groups, amino aldehyde groups, amino hydroxyl groups, amino carboxyl groups or amino phenol components.|INVENTION MODE|[0051] Detailed Description|[0052] The present invention is further illustrated below with reference to specific examples, which are intended to be illustrative only and not to limit the scope of the invention.|[0053] The embodiments of the present invention are described below with reference to specific embodiments, and other advantages and effects of the present invention will be easily understood by those skilled in the art from the disclosure of the present specification. The invention is capable of other and different embodiments and of being practiced or of being carried out in various ways, and its several details are capable of modification in various respects, all without departing from the spirit and scope of the present invention.|[0054] Example 1|[0055] Weighing 100g of wood activated carbon, and crushing the wood activated carbon into activated carbon powder of 200-300 meshes.|[0056] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 0.5h to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) with corresponding mass according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 0.5h to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.2, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 100g/L to obtain the sulfhydryl prepolymerization modified solution.|[0057] Weighing 10mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 1:100, and adding a proper amount of absolute ethyl alcohol as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at 70 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0058] And finally, drying the modified activated carbon at 80 ℃ for 6h, and then carrying out heat treatment at 350 ℃ for 2h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0059] Respectively filling raw wood activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 20 ℃, introducing ammonia-containing gas, controlling the pressure at 0.1MPa, controlling the concentration of an ammonia-containing compound at 10ppm, and controlling the airspeed at 500h-1The adsorption efficiency of the raw biomass activated carbon is 80 percent, the saturated adsorption capacity is 167mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 90 percent, and the saturated adsorption capacity is 213 mg/g.|[0060] Example 2|[0061] Weighing 100g of the shell activated carbon, and crushing the shell activated carbon into activated carbon powder of 200-300 meshes.|[0062] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 4 hours to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 4 hours to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.8, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 200g/L to obtain the sulfhydryl prepolymerization modified solution.|[0063] Weighing 150mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 30:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at the temperature of 90 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0064] And finally, drying the modified activated carbon at 110 ℃ for 48h, and then carrying out heat treatment at 600 ℃ for 6h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0065] Respectively filling raw fruit shell activated carbon and the sulfydryl modified activated carbon into a fixed bed reactor, controlling the reaction temperature at 80 ℃, introducing ammonia-containing gas, controlling the pressure at 10MPa, controlling the concentration of ammonia-containing compounds at 3000ppm, and controlling the airspeed at 20000h-1The adsorption efficiency of the original fruit shell activated carbon is 55 percent, the saturated adsorption capacity is 120mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 79 percent, and the saturated adsorption capacity is 209 mg/g.|[0066] Example 3|[0067] 100g of coal-based activated carbon is weighed and crushed into activated carbon powder of 300-400 meshes.|[0068] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 1 hour to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 3 hours to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.5, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 150g/L to obtain the sulfhydryl prepolymerization modified solution.|[0069] Weighing 66.7mL of sulfydryl pre-polymerization modified solution, placing the sulfydryl pre-polymerization modified solution in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified solution, wherein the mass ratio of the sulfydryl pre-polymerization modified solution to the activated carbon powder is 10:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at 80 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0070] And finally, drying the modified activated carbon at 100 ℃ for 36h, and then carrying out heat treatment at 500 ℃ for 4h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0071] Respectively filling raw coal activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 38 ℃, introducing ammonia-containing gas, controlling the pressure at 0.5MPa, controlling the concentration of ammonia-containing compounds at 100ppm, and controlling the airspeed at 6000h-1The adsorption efficiency of the raw coal-based activated carbon is 83 percent, the saturated adsorption capacity is 312mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 97 percent, and the saturated adsorption capacity is 423 mg/g.|[0072] Example 4|[0073] Weighing 100g of asphalt-based activated carbon, and crushing the asphalt-based activated carbon to 400-600 meshes of activated carbon powder.|[0074] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 2.5 hours to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) with corresponding mass according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 1.8h to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.4, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 100g/L to obtain the sulfhydryl prepolymerization modified solution.|[0075] Weighing 200mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 20:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at 85 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0076] And finally, drying the modified activated carbon at 90 ℃ for 24h, and then carrying out heat treatment at 400 ℃ for 3h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0077] Respectively filling the original asphalt-based activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 60 ℃, introducing ammonia-containing gas, controlling the pressure at 5MPa, controlling the concentration of an ammonia-containing compound at 1000ppm, and controlling the airspeed at 12000h-1The adsorption efficiency of the raw coal-based activated carbon is 85 percent, the saturated adsorption capacity is 267mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 98 percent, and the saturated adsorption capacity is 369 mg/g.|[0078] Example 5|[0079] 100g of synthetic resin-based activated carbon is weighed and crushed into activated carbon powder of 200-600 meshes.|[0080] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 2 hours to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) with corresponding mass according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 3.6h to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.7, and finally diluting the total prepolymer solution by using deionized water until the concentration of the total prepolymer solution is 120g/L to obtain the sulfhydryl prepolymerization modified solution.|[0081] Weighing 208mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 25:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at 80 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0082] And finally, drying the modified activated carbon at 95 ℃ for 38h, and then carrying out heat treatment at 450 ℃ for 3h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0083] Respectively filling the original synthetic resin-based activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 25 ℃, introducing ammonia-containing gas, controlling the pressure at 8MPa, controlling the concentration of ammonia-containing compounds at 700ppm and the space velocity at 9000h-1The adsorption efficiency of the raw coal-based activated carbon is 76%, the saturated adsorption capacity is 200mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 99%, and the saturated adsorption capacity is 397 mg/g.|[0084] Example 6|[0085] 100g of synthetic resin-based activated carbon is weighed and crushed into activated carbon powder of 200-600 meshes.|[0086] Mixing p-methylthiophenol, thiourea, formaldehyde and water, heating and stirring to obtain the sulfydryl prepolymerization modified solution. Specifically, p-methylthiophenol and formaldehyde solution (37 wt%) are weighed according to the molar ratio of p-methylthiophenol to formaldehyde of 1:2, an appropriate amount of deionized water is added, the mixture is heated and stirred at 70 ℃ for 3.5 hours to prepare a first prepolymer solution, and the first prepolymer solution is cooled for later use. And weighing thiourea and formaldehyde solution (37 wt%) according to the molar ratio of thiourea to formaldehyde being 1:2, adding a proper amount of deionized water, heating and stirring at 40 ℃ for 1h to prepare a second prepolymer solution, and cooling for later use. And then mixing the obtained first prepolymer solution and the second prepolymer solution to obtain a total prepolymer solution, wherein the mass ratio of the first prepolymer solution to the total prepolymer solution is 0.3, and finally diluting the mixture with deionized water until the concentration of the total prepolymer solution is 180g/L to obtain the sulfhydryl prepolymerization modified solution.|[0087] Weighing 83mL of sulfydryl pre-polymerization modified liquid, placing the sulfydryl pre-polymerization modified liquid in an open container, soaking activated carbon powder in the sulfydryl pre-polymerization modified liquid, wherein the mass ratio of the sulfydryl pre-polymerization modified liquid to the activated carbon powder is 15:100, and adding a proper amount of deionized water as a diluent to ensure that the activated carbon powder can be completely immersed in the diluted solution. Then, heating and stirring are carried out at the temperature of 90 ℃ until the solution is completely evaporated, thus obtaining the modified activated carbon.|[0088] And finally, drying the modified activated carbon at 105 ℃ for 14h, and then carrying out heat treatment at 580 ℃ for 3h in a nitrogen atmosphere to obtain the sulfydryl modified activated carbon.|[0089] Respectively filling the original synthetic resin-based activated carbon and the sulfydryl modified activated carbon adsorbent into a fixed bed reactor, controlling the reaction temperature at 30 ℃, introducing ammonia-containing gas, controlling the pressure at 0.6MPa, controlling the concentration of an ammonia-containing compound at 1500ppm, and controlling the airspeed at 5000h-1The adsorption efficiency of the raw coal-based activated carbon is 73 percent, the saturated adsorption capacity is 198mg/g, the adsorption efficiency of the sulfydryl modified activated carbon is 94 percent, and the saturated adsorption capacity is 302 mg/g.|[0090] In summary, the preparation method of the mercapto-modified activated carbon for removing malodorous gas provided by the invention can obtain the mercapto-modified activated carbon with uniformly distributed and controllable mercapto groups, further enhance the malodorous removal efficiency of the modified activated carbon, and is suitable for purification treatment of malodorous gas containing amino groups, amino aldehyde groups, amino hydroxyl groups, amino carboxyl groups or amino phenol components. Therefore, the invention effectively overcomes various defects in the prior art and has high industrial utilization value.|[0091] The foregoing embodiments are merely illustrative of the principles and utilities of the present invention and are not intended to limit the invention. Any person skilled in the art can modify or change the above-mentioned embodiments without departing from the spirit and scope of the present invention. Accordingly, it is intended that all equivalent modifications or changes which can be made by those skilled in the art without departing from the spirit and technical spirit of the present invention be covered by the claims of the present invention. Family Number|(85114797)|85114797|Abstract|(CN109967036B B)|The invention provides a preparation method of thiol - modified activated carbon for removal of stink . The method includes the steps of : 1 ) crushing activated carbon to prepare activated carbon powder ; 2 ) mixing p - toluenethiol , thiourea , formaldehyde and water , and then conducting heating and stirring to obtain a thiol pre - polymerized modified solution ; 3 ) conducting modification treatment on the activated carbon powder with the thiol pre - polymerized modified solution to obtain modified activated carbon ; and 4 ) drying the modified activated carbon and then conducting heat treatment to obtain theneeded thiol - modified activated carbon . The invention further provides the thiol - modified activated carbon prepared by the method and application thereof . The preparation method of the thiol - modifiedactivated carbon for removal of stink provided by the invention can acquire thiol - modified activated carbon with uniformly distributed and adjustable thiol , thus further enhancing the stink removal efficiency of the modified activated carbon . The thiol - modified activated carbon is suitable for purification treatment of malodorous gases containing ammonia amino , ammonia aldehyde group , ammonia hydroxyl , ammonia carboxyl or ammonia phenol components . |CPC codes|(CN109967036B B)|B01D - 053/02 |B01D - 2257/40 |B01J - 020/20 |B01J - 020/22 |IPC codes|(CN109967036B B)|B01D - 053/02 |B01J - 020/22 |B01J - 020/30 |Title|(CN109967036 A)|Preparation method of thiol - modified activated carbon for removal of stink | Chemical engineering|Environmental technology B01D-053/02|B01D-2257/40|B01J-020/20|B01J-020/22 B01D-053/02|B01D-2257/40|B01J-020/20|B01J-020/22 B01D-053/02|B01J-020/22|B01J-020/30 B01D-053/02|B01J-020/22|B01J-020/30 CN118384860|CN113952924|CN110935418 CN118384860 110801829 WHO=Examiner SELF=N CAT=A|CN113952924 98334621 WHO=Examiner SELF=N CAT=A|CN110935418 88057139 WHO=Examiner SELF=N CAT=A CN106847534|CN105771902|JP62114632 CN106847534 76433624 WHO=Examiner SELF=N|CN105771902 73635050 WHO=Examiner SELF=N|JP62114632 30679205 WHO=Examiner SELF=N S62114632 CN105771902; JP62114632; CN106847534 GRANTED (CN109967036)|GRANTED ALIVE (CN109967036)|ALIVE (CN109967036)|LEGAL DETAILS FOR CN109967036|Actual or expected expiration date=2037-12-28|Legal state=ALIVE|Status=GRANTED|Event publication date=2017-12-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201711461775|Application date=2017-12-28|Standardized application number=2017CN-1461775|Event publication date=2019-07-05|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN109967036|Publication stage code=A|Publication date=2019-07-05|Standardized publication number=CN109967036|Event publication date=2019-07-05|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2019-07-30|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2021-03-09|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN109967036|Publication stage code=B|Publication date=2021-03-09|Standardized publication number=CN109967036B|Event publication date=2021-03-09|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2024-04-02|Event code=CN/CP03|Event group=Change of name or address Reassignment|Change in the name or address of the patentee|FORMER APPLICANT:BIOMINTEC ENVIRONMENT TECH SHANGHAI CO LTD APPLICANT:Baimei Smart Technology (Shanghai) Co.,Ltd. (CN109967036)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjk8tgRGOPo5Fxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=WmyfX000ib20so9TkpahM7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN109967036)|CN|(CN109967036)|CN (CN109967036)|NAME=BIOMINTEC ENVIRONMENT TECH SHANGHAI CO LTD , COUNTRY=CN|(CN109967036)|NAME=BIOMINTEC ENVIRONMENT TECH SHANGHAI CO LTD , COUNTRY=CN (CN109967036)|NAME=XU YILIN;JZMC PATENT AND TRADEMARK LAW OFFICE , REG=31219|(CN109967036)|NAME=XU YILIN;JZMC PATENT AND TRADEMARK LAW OFFICE , REG=31219 (CN109967036)|CN|(CN109967036)|CN (CN109967036)|NAME=XU QIAN, COUNTRY=CN |NAME=LI JUN|(CN109967036)|NAME=XU QIAN, COUNTRY=CN |NAME=LI JUN 0 1 Titre: (CN109967036)|Preparation method of sulfydryl modified activated carbon for removing malodor Résumé: (CN109967036)|The invention provides a preparation method of thiol-modified activated carbon for removal of stink. The method includes the steps of: 1) crushing activated carbon to prepare activated carbon powder;2) mixing p-toluenethiol, thiourea, formaldehyde and water, and then conducting heating and stirring to obtain a thiol pre-polymerized modified solution; 3) conducting modification treatment on the activated carbon powder with the thiol pre-polymerized modified solution to obtain modified activated carbon; and 4) drying the modified activated carbon and then conducting heat treatment to obtain theneeded thiol-modified activated carbon. The invention further provides the thiol-modified activated carbon prepared by the method and application thereof. The preparation method of the thiol-modifiedactivated carbon for removal of stink provided by the invention can acquire thiol-modified activated carbon with uniformly distributed and adjustable thiol, thus further enhancing the stink removal efficiency of the modified activated carbon. The thiol-modified activated carbon is suitable for purification treatment of malodorous gases containing ammonia amino, ammonia aldehyde group, ammonia hydroxyl, ammonia carboxyl or ammonia phenol components. 51 Abstract gpt-4o-mini no The article focuses on a method for preparing thiol-modified activated carbon for removing odors, which does not relate to accelerated weathering or CO₂ capture.
53 CN202511126466 CN202511126466 CN120903536 116599289 CN120903536 A 2025-11-07 [CN120903536] 2025-08-12 2025-08-12 2025-11-07 (CN120903536)|2045-08-12 (CN120903536)|Method and device for realizing carbon sequestration of red mud under supercritical condition (CN120903536)|The invention discloses a method and a device for realizing red mud carbon sequestration under supercritical conditions, and relates to the technical field of red mud carbon sequestration, the method comprises a red mud pretreatment step, an ultrasonic cavitation crushing step and a microchannel mixing reaction step, the device comprises a pretreatment unit, an ultrasonic crushing module, a micro-channel mixing module, a gradient reaction tower, a temperature and pressure control system, a multi-stage reciprocating compressor and an external circulating pump. An ultrasonication area is arranged at the top, a honeycomb-shaped micro-channel mixing module is integrated in the middle, a gradient temperature reaction tower is arranged at the bottom, a baffle plate is arranged for strengthening mass transfer, and after a carbon sequestration reaction is completed, slurry returns to the reaction area through a circulating pump; the particle size of the red mud is reduced to 1-5 [mu] m through the ultrasonic-microchannel synergistic effect, and three-phase mixing of the red mud and supercritical CO2 is completed within 0.5 s; meanwhile, a porous supported calcium-magnesium composite catalyst is adopted, the confinement effect and hydrophobicity of a carrier are utilized, the carbon sequestration efficiency is improved to 95% or above, and the problem of silicate side reaction caused by too strong alkalinity is solved. KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY (CN120903536)|KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) HUANG JIANHONG|JIANG ZHUOLUN|ZUO JIANFEN|LUO QIULI|ZHU BIN|XIE XIN|TIAN SENLIN|ZHAO QUN|LI JIE (CN120903536)|HUANG JIANHONG|JIANG ZHUOLUN|ZUO JIANFEN|LUO QIULI|ZHU BIN|XIE XIN|TIAN SENLIN|ZHAO QUN|LI JIE (CN120903536)|WANG YUKUI;Kunming Longhe Intellectual Property Agency (General Partnership)|Reg. Nb: 53220 (CN120903536)|As a further improvement of the present invention, the porous supported catalyst in step S4 is prepared by the steps of:|The supercritical CO _2 technology generates stable carbonate by reacting supercritical CO _2 with alkaline components in red mud, achieves the aim of 'carbon fixation by waste', and has the advantages of carbon sequestration and red mud harmless utilization.|Meanwhile, compared with the prior art, the single calcium-based catalyst is used, the local pH is too high due to the too strong alkalinity, and silicate side reaction is initiated (silicate reacts with alkaline substances to generate silicate complex, alkaline substances are consumed, so that carbonate generation is reduced, and carbon fixing efficiency is affected).| (CN120903536)|1. The method for realizing carbon fixation of the red mud under the supercritical condition is characterized by comprising the following steps of: S1, cleaning red mud, drying to remove free moisture, crushing the dried red mud to form dried red mud powder, and mixing the dried red mud powder with deionized water in proportion; S2, pressurizing CO 2 to supercritical pressure and supercritical temperature; s3, ultrasonically crushing the slurry obtained in the step S1, and carrying out cavitation crushing through an ultrasonic array to reduce the particle size of the red mud; S4, the crushed slurry, the pressurized supercritical CO 2 in the step S2 and the porous supported catalyst are mixed in a honeycomb microchannel in a three-phase manner, wherein the mixing time is less than or equal to 0.5 seconds; s5, the mixed materials enter a gradient reaction tower, and are subjected to carbon fixation reaction under the condition of sectional temperature control and then cooled. | (CN120903536)|The invention discloses a method and a device for realizing red mud carbon fixation under supercritical conditions, which relate to the technical field of red mud carbon fixation, the method comprises a red mud pretreatment step, an ultrasonic cavitation crushing step and a microchannel mixing reaction step, the device comprises a pretreatment unit, an ultrasonic crushing module, a micro-channel mixing module, a gradient reaction tower, a temperature and pressure control system, a multistage reciprocating compressor and an external circulating pump.|The invention mainly aims to provide a method and a device for realizing carbon fixation of red mud under supercritical conditions, which are used for solving the problem of red mud recycling treatment.In order to achieve the above purpose, the invention provides a method for realizing carbon fixation of red mud under supercritical conditions, which comprises the following steps:|The invention relates to the technical field of red mud carbon fixation, in particular to a method and a device for realizing red mud carbon fixation under supercritical conditions.| (CN120903536)|RED MUD(100,133)|SUPERCRITICAL CONDITION(100,16)|REALIZING CARBON FIXATION(100,10)|ULTRASONIC CAVITATION CRUSHING(96,1)|GRADIENT REACTION TOWER(73,44)|CAVITATION CRUSHING(68,1)|HONEYCOMB MICROCHANNEL(61,5)|RED MUD ANNULAR DISTRIBUTOR(58,27)|RED MUD PRETREATMENT(49,1)|ULTRASONIC CRUSHING MODULE(46,5)|ALKALINE SUBSTANCE(46,2)|RED MUD HARMLESS UTILIZATION(46,1)|MULTISTAGE RECIPROCATING COMPRESSOR(43,16)|HARMLESS UTILIZATION(42,1)|ULTRASONIC CRUSHING ZONE(42,1)|MICROCHANNEL(41,5)|TOO STRONG ALKALINITY(34,1)|RED MUD RECYCLING TREATMENT(33,1)|CRUSHED SLURRY(32,11)|PIEZOELECTRIC CERAMIC TRANSDUCER(32,3)|CARBON FIXATION(31,31)|DRIED RED MUD(31,10)|RED MUD DRYING TOWER(30,10)|CARRIER IMPREGNATION(30,9)|RED MUD CARBON FIXATION(30,3)|RECYCLING TREATMENT(30,1)|CONICAL COLLECTOR(29,7)|CARBONATE GENERATION(29,1)|SILICATE COMPLEX(29,1)|SUPPORTED CATALYST POROSITY(27,25)|PRETREATMENT(26,2)|CARRIER HYDROPHOBICITY(25,2)|RED MUD POWDER(24,6)|CLEANING RED MUD(24,3)|DRIED RED MUD POWDER(24,3)|GRADIENT CALCINATION(24,3)|DECOMPOSE NITRATE(23,4)|ANNULAR RED MUD DISTRIBUTOR(23,2)|DOMAIN LIMITING(23,1)|BAFFLE PUMP(22,1)|CARBON FIXATION REACTION(21,4)|TITANIUM ALLOY AMPLITUDE TRANSFORMER(20,6)|SUPERCRITICAL TEMPERATURE(20,3)|CIRCULATING PUMP(19,9)|MGO CAO NANO PARTICLE(19,4)|CAVITATION(19,3)|HONEYCOMB SHAPED MICROCHANNEL(19,1)|CALCIUM MAGNESIUM COMPOSITE CATALYST(18,6)|CRUSHED RED MUD(18,5)|GRADIENT TEMPERATURE REACTION TOWER(18,1)|REACTION ZONE(18,1)|PRESSURIZING(17,12)|ALKALINE COMPONENT(17,2)|HEXAMETHYLDISILAZANE(17,2)|CARBON SEQUESTRATION(17,1)|SINGLE CALCIUM CATALYST(17,1)|SLURRY(16,12)|ULTRASONIC TRANSDUCER(16,11)|CENTRIFUGALLY COLLECTING WHITE PRECIPITATE(15,3)|ANNULAR DISTRIBUTION(15,2)|MICROCHANNEL MIXING MODULE(15,1)|DYNAMIC AMPLITUDE REGULATION RANGE(14,1)|MIXING CYLINDER OUTSIDE(13,7)|DRY RED MUD POWDER(13,3)|SILICATE(13,3)|ULTRASONIC ARRAY(13,3)|BUTT EDGE(13,2)|MASS TRANSFER ENHANCEMENT(13,1)|BALL MILL(12,20)|MOLAR RATIO(12,4)|CARBON FIXING(10,4)|GRADIENT REACTION TOWER TOP(10,3)|DRYING TEMPERATURE(10,2)|DEIONIZED WATER(9,8)|MULTILAYER MICROCHANNEL(9,7)|MAGNESIUM NITRATE(9,4)|SOL GEL(9,4)|STABLE OXIDE(9,4)|PARTICLE SIZE(8,15)|ACIDOLYSIS(8,8)|ULTRASONIC CRUSHING AREA(8,8)|ZINC ACETATE DIHYDRATE(8,7)|CALCIUM NITRATE(8,4)|GAS PHASE HYDROPHOBIC MODIFICATION(8,4)|SUPERCRITICAL PRESSURE(8,3)|CARBONATE CRYSTAL NUCLEUS(8,2)|DEEP CARBONIZATION(8,2)|REACTION TEMPERATURE(7,3)|TOTAL MOLAR MASS(7,3)|CARBON FIXATION RATE(6,11)|MIXED MATERIAL(6,9)|CARBONATE ION(6,3)|RED MUD SLURRY(6,3)|SILICATE SIDE REACTION(6,3)|MIDDLE TEMPERATURE REGION(6,2)|EXTENSIVE UTILIZATION(6,1)|REACTION STEP(6,1)|RED MUD COMPREHENSIVE UTILIZATION(6,1)|ULTRASONIC CAVITATION(6,1)|REACTION PRESSURE(5,12)|MIDDLE LAYER(5,8)|BAFFLE PLATE(5,7)|WATER INLET PIPE(5,6)|CARRIER POWDER(5,4)|CATALYST FEED PIPE(5,3)|HYDROPHOBICITY(5,3)|GRADIENT CIRCULATION PUMP(5,2)|OVER STRONG ALKALINITY(5,2)|CARRIER PORE CANAL(5,1)|DEHYDRATE IMPREGNATING SOLUTION(5,1)|RED MUD ALKALINITY(5,1)|ALUMINUM PLANT(4,6)|NANOSCALE(4,2)|TITANATE(4,2)|CARBONATE PRECIPITATE(4,1)|CARBONATE PRECIPITATION(4,1)|FINE GRANULARITY(4,1)|MAGNESIUM CATALYST(4,1)|PRETREATED RED MUD(4,1)|QUANTITATIVE CALCULATION(4,1)|RED MUD CORROSION LIFE(4,1)|STABLE MGCO(4,1)|UNEVEN STIRRING(4,1)|THREE PHASE(3,7)|COOLING WATER JACKET(3,4)|LIQUID SOLID RATIO(3,3)|OVEN(3,3)|STANDING(3,3)|190 MESH SIEVE(3,1)|ACCURATE PARTITION(3,1)|FEEDBACK PIPE(3,1)|INERTNESS(3,1)|INSTANTANEOUS MIXING(3,1)|LANDFILL(3,1)|REACTED RED MUD SAMPLE(3,1)|REACTOR WORK(3,1)|SOLUBLE DIVALENT CATION(3,1)|TON RED MUD TREATMENT(3,1)|ULTRASONIC TREATMENT(3,1)|160 MESH SIEVE(2,1)| (CN120903536)|1. The method for realizing carbon fixation of the red mud under the supercritical condition is characterized by comprising the following steps of:| S1, cleaning red mud, drying to remove free moisture, crushing the dried red mud to form dried red mud powder, and mixing the dried red mud powder with deionized water in proportion; | S2, pressurizing CO 2 to supercritical pressure and supercritical temperature; | s3, ultrasonically crushing the slurry obtained in the step S1, and carrying out cavitation crushing through an ultrasonic array to reduce the particle size of the red mud; | S4, the crushed slurry, the pressurized supercritical CO 2 in the step S2 and the porous supported catalyst are mixed in a honeycomb microchannel in a three-phase manner, wherein the mixing time is less than or equal to 0.5 seconds; | s5, the mixed materials enter a gradient reaction tower, and are subjected to carbon fixation reaction under the condition of sectional temperature control and then cooled. |2. The method for realizing carbon fixation of red mud under supercritical conditions according to claim 1, wherein in the step S1, the drying temperature is T1, the temperature is 100 ℃ and less than or equal to T1 and less than 120 ℃, the dried red mud is crushed to 150-200 meshes, and the crushed red mud is mixed with deionized water according to a liquid-solid ratio of 8-10:1.|3. The method for realizing carbon fixation of red mud under supercritical conditions according to claim 1, wherein the supercritical CO 2 reaction pressure in the step S2 is P1,10MPa < P1 is less than or equal to 25MPa, and the supercritical CO 2 reaction temperature in the step S3 is T2, and the temperature is 35 ℃ and is less than or equal to 80 ℃.|4. The method for realizing carbon fixation of red mud under supercritical conditions according to claim 1, wherein the ultrasonic crushing in the step S3 adopts a piezoelectric ceramic transducer with the frequency of 40 kHz, and the dynamic amplitude regulation range is 10-100%, so that the particle size of the red mud is reduced to 1-5 μm.|5. The method for realizing carbon sequestration of red mud under supercritical conditions according to claim 1, wherein the porous supported catalyst added in the step S4 is added in an amount of 2-10wt% of the dry red mud powder.|6. The method for realizing carbon fixation of red mud under supercritical conditions according to claim 1 or 5, wherein the porous supported catalyst in the step S4 is prepared by the following steps:| (1) Synthesizing a carrier by using zinc acetate dihydrate, 2-methylimidazole and methanol by a sol-gel method; | (2) Preparing an impregnating solution with the total molar mass of 1.5mol/L by using calcium nitrate and magnesium nitrate according to the molar ratio of Ca to Mg=2:1, and impregnating the carrier in the impregnating solution to obtain an impregnated carrier; | (3) And (3) placing the impregnated carrier in an N 2 atmosphere for gradient calcination, calcining at 100-150 ℃ for 1-2 hours to dehydrate, calcining at 300-400 ℃ for 2-3 hours to decompose nitrate to generate MgO/CaO nano-particles, calcining at 550-650 ℃ for 3-4 hours to form stable oxide in the impregnated carrier, and performing gas phase hydrophobic modification on the hexamethyldisilazane to obtain the porous supported catalyst. |7. The method for realizing carbon fixation of red mud under supercritical conditions according to claim 1, wherein the honeycomb-shaped micro-channels in the step S4 are micro-channel mixing modules, and are formed by stacking a plurality of layers of titanium alloy micro-channel plates, and each single plate comprises 800-4000 regular hexagon flow channels with a butt edge distance of 50-300 μm.|8. The method for realizing carbon fixation of red mud under supercritical conditions according to claim 1, wherein the temperature of the upper low-temperature region of the gradient reaction tower in the step S5 is 35-50 ℃, the temperature of the middle-temperature region is 50-65 ℃, and the temperature of the lower high-temperature region is 65-80 ℃.|9. The device for realizing red mud carbon fixation under the supercritical condition according to claim 1 is characterized by comprising a red mud drying tower, a ball mill communicated with the red mud drying tower, a mixing outer cylinder arranged at an outlet of the ball mill, a first red mud annular distributor, a second red mud annular distributor and a CO 2 annular distributor arranged in the mixing outer cylinder from top to bottom, an ultrasonic transducer and a titanium alloy amplitude transformer vertically arranged between the first red mud annular distributor and the second red mud annular distributor, a multi-layer micro-channel mixing module arranged between the second red mud annular distributor and the CO 2 annular distributor, a gradient reaction tower arranged below the CO 2 annular distributor, a multi-stage reciprocating compressor connected outside the CO 2 annular distributor, a plurality of groups of plates arranged in the gradient reaction tower at intervals, a pressure relief valve arranged on the outer wall of the gradient reaction tower, a catalyst arranged at the top end of the gradient reaction tower, a water inlet pipe arranged on the first red mud annular distributor and a temperature and pressure control system arranged outside the gradient reaction tower, a conical collector arranged at the bottom of the gradient reaction tower, a circulating pump connected outside the conical collector, and a baffle pump connected to the top of the gradient reaction tower.|10. The device for realizing carbon sequestration of red mud under supercritical conditions according to claim 9, wherein the annular CO 2 distributor is provided with nozzles in an annular distribution, the caliber of the nozzles is 0.1-0.5 mm, and the nozzles are arranged towards the second annular red mud distributor, so that CO 2 flowing in the annular CO 2 distributor flows from the bottom end of the multi-layer micro-channel mixing module towards the ultrasonic transducer. (CN120903536)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of red mud carbon fixation, in particular to a method and a device for realizing red mud carbon fixation under supercritical conditions.|BACKGROUND ART|[0002] Red mud is an industrial solid waste produced in the alumina production process. It has the characteristics of strong alkalinity, heavy metal content, high viscosity, fine granularity and the like. Long-term storage only occupies a large amount of land, and also can pollute water and soil. Therefore, a large amount of red mud is a solid waste which is needed to be treated and is urgently needed to be recycled, and the red mud is used as industrial solid waste with extremely high yield, and the problems of high carbon emission, potential resource waste of the red mud and the like exist in the traditional landfill, stockpiling or neutralization method. The supercritical CO 2 technology generates stable carbonate by reacting supercritical CO 2 with alkaline components in red mud, achieves the aim of 'carbon fixation by waste', and has the advantages of carbon sequestration and red mud harmless utilization.|DISCLOSURE|Disclosure of Invention|[0003] The invention mainly aims to provide a method and a device for realizing carbon fixation of red mud under supercritical conditions, which are used for solving the problem of red mud recycling treatment.|[0004] In order to achieve the above purpose, the invention provides a method for realizing carbon fixation of red mud under supercritical conditions, which comprises the following steps:| S1, cleaning red mud, drying to remove free moisture, crushing the dried red mud to form dried red mud powder, and mixing the dried red mud powder with deionized water in proportion; | S2, pressurizing CO 2 to supercritical pressure and supercritical temperature; | s3, ultrasonically crushing the slurry obtained in the step S1, and carrying out cavitation crushing through an ultrasonic array to reduce the particle size of the red mud; | S4, the crushed slurry, the pressurized supercritical CO 2 in the step S2 and the porous supported catalyst are mixed in a honeycomb microchannel in a three-phase manner, wherein the mixing time is less than or equal to 0.5 seconds; | s5, the mixed materials enter a gradient reaction tower, and are subjected to carbon fixation reaction under the condition of sectional temperature control and then cooled. |[0005] As a further improvement of the invention, in the step S1, the drying temperature is T1, the temperature is 100 ℃ less than or equal to T1 and less than 120 ℃, the dried red mud is crushed to 150-200 meshes, and the crushed red mud is mixed with deionized water according to a liquid-solid ratio of 8-10:1.|[0006] As a further improvement of the invention, the supercritical CO 2 reaction pressure in the step S2 is P1,10MPa < P1 is less than or equal to 25MPa, and the supercritical CO 2 reaction temperature in the step S3 is T2, wherein the temperature of 35 ℃ is less than or equal to 80 ℃.|[0007] As a further improvement of the invention, in the step S3, the piezoelectric ceramic transducer with the frequency of 40 kHz is adopted for ultrasonic crushing, and the dynamic amplitude regulation and control range is 10-100%, so that the particle size of the red mud is reduced to 1-5 mu m.|[0008] As a further improvement of the invention, the addition amount of the porous supported catalyst added in the step S4 is 2-10wt% of the dry red mud powder.|[0009] As a further improvement of the present invention, the porous supported catalyst in step S4 is prepared by the steps of:| (1) The method comprises the steps of adopting a sol-gel method to synthesize a carrier by utilizing zinc acetate dihydrate, 2-methylimidazole and methanol, weighing 20 g zinc acetate dihydrate, dissolving in 400 mL methanol to form a solution A, weighing 30 g of 2-methylimidazole, dissolving in 400 mL methanol to obtain a solution B, rapidly mixing the solution A and the solution B, stirring 12 h at 25 ℃, standing and aging 24 h, centrifugally collecting white precipitate, washing the white precipitate with methanol for 3 times, and drying 12 h at 80 ℃ in an oven to obtain carrier powder; | (2) Preparing an impregnating solution with the total molar mass of 1.5mol/L by using calcium nitrate and magnesium nitrate according to the molar ratio of Ca to Mg=2:1, and impregnating the carrier in the impregnating solution to obtain an impregnated carrier; | (3) And (3) placing the impregnated carrier in an N 2 atmosphere for gradient calcination, calcining at 100-150 ℃ for 1-2 hours to dehydrate, calcining at 300-400 ℃ for 2-3 hours to decompose nitrate to generate MgO/CaO nano-particles, calcining at 550-650 ℃ for 3-4 hours to form stable oxide in the impregnated carrier, and performing gas phase hydrophobic modification on the carrier to obtain the porous supported catalyst, wherein the water contact angle of the porous supported catalyst is more than 130 degrees, and the porous supported catalyst has strong hydrophobicity. |[0010] As a further improvement of the invention, the honeycomb microchannel in the step S4 is a microchannel mixing module, and is formed by stacking a plurality of layers of titanium alloy microchannel plates, and the single plate comprises 800-4000 regular hexagon flow channels with the opposite side distance of 50-300 mu m.|[0011] As a further improvement of the invention, in the step S5, the temperature of the upper low temperature region of the gradient reaction tower is 35-50 ℃, carbonate crystal nucleus is generated, the temperature of the middle temperature region is 50-65 ℃, crystal growth is promoted, and the temperature of the lower high temperature region is 65-80 ℃, and deep carbonization is carried out.|[0012] The device comprises a red mud drying tower, a ball mill communicated with the red mud drying tower, and a mixing outer cylinder arranged at an outlet of the ball mill, wherein a first red mud annular distributor, a second red mud annular distributor and a CO 2 annular distributor are arranged in the mixing outer cylinder from top to bottom, an ultrasonic transducer and a titanium alloy amplitude transformer are vertically arranged between the first red mud annular distributor and the second red mud annular distributor, a multi-layer microchannel mixing module is arranged between the second red mud annular distributor and the CO 2 annular distributor, a gradient reaction tower is arranged below the CO 2 annular distributor, a multi-stage reciprocating compressor is connected outside the CO 2 annular distributor, a plurality of groups of baffle plates are arranged in the gradient reaction tower at intervals, a pressure relief valve is arranged on the outer wall of the gradient reaction tower, a catalyst feed pipe is arranged at the top end of the gradient reaction tower, a water inlet pipe and a red mud feed pipe communicated with the ball mill are arranged on the first red mud annular distributor, a temperature and pressure control system is arranged outside the gradient reaction tower, a conical collector is arranged at the bottom end of the gradient reaction tower, a circulating pump is connected outside the conical collector, and the top of the gradient reaction tower is communicated with the circulating pump.|[0013] As a further improvement of the invention, the CO 2 annular distributor is annularly distributed with nozzles with the caliber of 0.1-0.5 mm, and the nozzles are arranged towards the second red mud annular distributor so that CO 2 flowing in the CO 2 annular distributor flows from the bottom end of the multi-layer micro-channel mixing module towards the ultrasonic transducer.|[0014] The beneficial effects of the invention are as follows:| 1. The invention can ensure that CO 2 maintains high diffusivity of gas under the condition of supercritical CO 2, simultaneously obtains strong dissolving capacity of liquid, has chemical inertness and mildness, can fully diffuse, fully contact with red mud, react with pore water or alkaline components in the red mud to generate carbonate ions, dissolve alkaline metal oxides (such as CaO) in the red mud to generate corresponding hydroxides, release soluble divalent metal ions (such as Mg 2+、Ca2+), and react with the carbonate ions to generate carbonate precipitates. The process not only can realize the aim of fixing carbon in the red mud, but also can reduce the alkalinity of the red mud, and is ready for the subsequent comprehensive utilization of the red mud. |[0015] 2. The invention only uses a supercritical CO 2 system, and does not use supercritical water and supercritical CO 2 to be applied in a combined way, but adopts a mode of adding a porous supported calcium-magnesium composite catalyst. The elimination of supercritical water can reduce the energy consumption of the whole reaction, and the water needs to reach a high temperature and a high pressure of >374 ℃ and >22.1MPa to reach a supercritical state, so that the whole reaction can be realized under milder conditions by using only supercritical CO 2. Titanate and silicate existing in the red mud compete with carbonate ions for soluble divalent cations (such as Ca 2+、Mg2+) in the red mud, which can be used for generating carbonate precipitation, so that the porous supported calcium-magnesium composite catalyst is added during the reaction, the competition between the titanate and silicate in the red mud is reduced, and the carbonate precipitation is easier to generate and the carbon fixing efficiency is higher. Meanwhile, compared with the prior art, the single calcium-based catalyst is used, the local pH is too high due to the too strong alkalinity, and silicate side reaction is initiated (silicate reacts with alkaline substances to generate silicate complex, alkaline substances are consumed, so that carbonate generation is reduced, and carbon fixing efficiency is affected). The alkaline (pH is about 10.3) of MgO is slightly lower than that of CaO (pH is about 12.5), and the pH is regulated and controlled by adding the magnesium-based catalyst, so that the generation of byproducts is reduced, and the carbon fixing efficiency is improved by more than 20%. In addition, mgO is more stable in a supercritical CO 2 environment, the combination capability of Mg 2+ and CO 32+ is stronger, and more stable MgCO 3 precipitate can be generated, so that the carbon fixing effect is better.|[0016] 3. The porous supported calcium-magnesium composite catalyst used in the invention is prepared by a sol-gel method, and a carrier is synthesized by zinc acetate dihydrate, 2-methylimidazole and methanol. Dissolving 20 g zinc acetate dihydrate in 400mL of methanol to form a solution A, dissolving 30 g of 2-methylimidazole in 400mL of methanol to obtain a solution B, rapidly mixing the solution A and the solution B, stirring the solution B at 25 ℃ for 12h, standing and aging the solution B for 24h, centrifugally collecting white precipitate, washing the white precipitate with methanol for 3 times, drying the white precipitate at 80 ℃ in an oven for 12h to obtain carrier powder, preparing calcium nitrate and magnesium nitrate into 1.5mol/L impregnating solution according to the molar ratio of Ca to Mg=2:1, loading the impregnating solution in an equal volume, calcining the impregnating solution in a gradient manner at 120 ℃,350 ℃ and 600 ℃ under the atmosphere of N 2, calcining the solution B at 120 ℃ for 2h to dehydrate the impregnating solution, calcining the solution B at 350 ℃ for 3h to decompose nitrate to generate MgO/CaO nano particles, calcining the red mud at 600 ℃ for 4h to form stable oxide, and finally performing gas phase hydrophobic modification on the hexamethyldisilazane to enable the water contact angle to be more than 130 ℃, so that the carrier powder has strong hydrophobicity, and prevents corrosion in the slurry and prevents catalyst from being deactivated.|[0017] 4. The porous supported calcium-magnesium composite catalyst used in the invention has a carrier pore canal of only 1.2nm, and limits CaO/MgO active components to nano-scale to form a high-density catalytic microreactor, so that the diffusion distance of CO 2 is shortened to nano-scale, and the carbon fixation rate is greatly improved. In addition, since silicate diameters are generally greater than 1.5nm, it is blocked by the support pore channels and eliminates competing side reactions.|[0018] 5. The reactor of the device adopts the combination of ultrasonic crushing, micro-channel mixing and gradient reaction towers, the reaction takes more than 30 minutes and the carbon fixation rate is only 89.5 percent due to uneven stirring in the traditional method, the device crushes red mud to the level of 1-5 mu m through 40 kHz ultrasonic cavitation, the mass transfer efficiency is improved by 60 times by combining with supercritical CO 2 turbulence in a honeycomb micro-channel, the reaction time is shortened to be within 10 minutes, and meanwhile, the three-section gradient temperature control reaction towers (35-80 ℃ accurate partition) cooperate with a catalyst with the finite field effect, so that the carbon fixation rate is improved to 95.5 percent, the ton red mud treatment energy consumption is only 120 kWh, and the traditional device is up to 200 kWh and has serious side reaction.|DRAWINGS DESCRIPTION|[0019] FIG. 1 is a schematic diagram of an apparatus used in the method for implementing carbon fixation of red mud under supercritical conditions;| Reference numerals illustrate: | 1. the device comprises a red mud drying tower, a ball mill, a3, a mixing outer cylinder, a 4, a first red mud annular distributor, a 5, a second red mud annular distributor, a 6, CO 2 annular distributor, a 7, an ultrasonic transducer, an 8, titanium alloy amplitude transformer, a 9, a multi-layer microchannel mixing module, a 10, a gradient reaction tower, a 11, a multi-stage reciprocating compressor, a 12, a baffle plate, a 13, a pressure relief valve, a 14, a catalyst feeding pipe, a 15, a water inlet pipe, a 16, a red mud feeding pipe, a 17, a temperature and pressure control system, a 18, a conical collector, a 19, a circulating pump, a 20 and a cooling water jacket. |INVENTION MODE|Detailed Description|[0020] The present application will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present application more apparent. It should be understood that the described embodiments are merely some, but not all embodiments of the present application. Embodiments of the application and features of the embodiments may be combined with each other without conflict. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to be within the scope of the application.|[0021] The invention discloses a method for realizing carbon fixation of red mud under supercritical conditions, which comprises the following steps:| S1, cleaning red mud, sending the red mud into a drying tower to remove free moisture, crushing the dried red mud by a ball mill 2 to form dried red mud powder, and mixing the dried red mud powder with deionized water in proportion; | S2, pressurizing CO 2 to supercritical pressure and supercritical temperature in a compressor; | S3, sending the slurry obtained in the step S1 into an ultrasonic crushing area, and carrying out cavitation crushing through an ultrasonic array to reduce the particle size of the red mud; | S4, enabling crushed slurry, pressurized supercritical CO 2 in the step S2 and the porous supported catalyst to enter a micro-channel mixing module in parallel, and completing three-phase mixing in a honeycomb micro-channel, wherein the mixing time is less than or equal to 0.5 seconds; | S5, the mixed materials enter a gradient reaction tower 10, carbon fixation reaction is carried out under the condition of sectional temperature control, and the temperature is reduced after the reaction is carried out for 10 min. |[0022] In order to ensure that supercritical CO 2, porous supported catalyst and crushed slurry are fully contacted, referring to fig. 1, the device further comprises a red mud drying tower 1, a ball mill 2 communicated with the red mud drying tower 1, a mixing outer cylinder 3 arranged at an outlet of the ball mill 2, a first red mud annular distributor 4, a second red mud annular distributor 5 and a CO 2 annular distributor 6 are arranged in the mixing outer cylinder 3 from top to bottom, an ultrasonic transducer 7 and a titanium alloy amplitude transformer 8 are vertically arranged between the first red mud annular distributor 4 and the second red mud annular distributor 5, a multi-layer micro-channel mixing module 9 is arranged between the second red mud annular distributor 5 and the CO 2 annular distributor 6, a gradient reaction tower 10 is arranged below the CO 2 annular distributor 6, a multistage reciprocating compressor 11 is connected to the outside of the CO 2 annular distributor 6, a plurality of groups of baffle plates 12 are arranged in the gradient reaction tower 10 at intervals, a pressure relief valve 13 is arranged on the outer wall of the gradient reaction tower 10, a catalyst feed pipe 14 is arranged at the top end of the gradient reaction tower 10, a feed pipe 16 is vertically arranged between the first annular distributor 4 and the second red mud annular distributor 5, a temperature control system 17 is arranged outside the gradient reaction tower 10, a conical collector 18 is arranged at the bottom of the gradient reaction tower 10, and a gradient circulation pump 19 is connected to the top of the gradient reaction tower 18 is connected to the gradient circulation pump 19.|[0023] The device comprises a red mud drying tower 1, a ball mill 2, a red mud feeding pipe 16, a water inlet pipe 15, a first red mud annular distributor 4, a second red mud annular distributor 5, an ultrasonic transducer 7, a titanium alloy amplitude transformer 8, a catalyst feeding pipe 14, a multi-layer micro-channel mixing module 9, a CO 2 annular distributor 6, a gradient reaction tower 10, a baffle plate 12, a multi-stage reciprocating compressor 11, a pressure relief valve 13, a temperature and pressure control system 17, a circulating pump 19, a cooling water jacket 20 and a conical collector 18, wherein the ultrasonic transducer 7 and the titanium alloy amplitude transformer 8 are arranged in a closed tubular structure and are vertically arranged, the upper end of the ultrasonic transducer is provided with the red mud feeding pipe 16 and the water inlet pipe 15, the two pipes are respectively fed with dried and crushed red mud and deionized water, the dried and crushed red mud are mixed and enter the first red mud annular distributor 4 to ensure that red mud slurry uniformly enters an ultrasonic crushing stage, the red mud slurry after ultrasonic crushing passes through a second red mud annular distributor 5 arranged at the lower end and then uniformly enters a multi-layer micro-channel mixing module 9, the multi-layer micro-channel mixing module 9 is arranged in a closed tubular structure, the multi-layer micro-channel mixing module 9 is connected with the ultrasonic crushing module through the second red mud annular distributor 5, a catalyst feeding pipe 14 is arranged at the upper end, a CO 2 annular distributor 6 is arranged at the lower end, a catalyst and supercritical CO 2 respectively enter the multi-layer micro-channel mixing module 9 from the two ends, three phases are instantaneously mixed through micro-channels, the mixed slurry enters a gradient reaction tower 10 connected below the multi-layer micro-channel mixing module 9, carbonate crystal nuclei are generated in an upper low temperature region (35-50 ℃) of the gradient reaction tower 10, crystal growth is promoted in a middle medium temperature region (50-65 ℃) and deep carbonization is completed in a lower high temperature region (65-80 ℃), the temperature is controlled by a temperature pressure control system 17. The baffle plates 12 are arranged in the gradient reaction tower 10, and 8-10 pieces are arranged from top to bottom. The pressure release valve 13 is used for releasing pressure when the reaction pressure is exceeded to ensure safety, and the multistage reciprocating compressor 11 is used for pressurizing CO 2 to supercritical CO 2 reaction pressure and then uniformly inputting the CO 2 reaction pressure into the multilayer microchannel mixing module 9 through the CO 2 annular distributor 6.|[0024] Preferably, the outer layer of the ultrasonic crushing module is provided with a cooling water jacket 20 to prevent the temperature from being too high during ultrasonic treatment.|[0025] Preferably, the ultrasonic crushing module has a height of 1.5 m, a diameter of 1m, an ultrasonic transducer 7 diameter of 300 mm, a length of 200 mm (including a horn), a cooling water jacket 20 wall thickness of 2 mm and a sandwich inner diameter of 8 mm.|[0026] Preferably, the multilayer microchannel mixing module 9 has a height of 1.8 m and a diameter of 1. 1m, and a single-layer microchannel plate thickness of 100. 100 mm and a diameter of 0.98 m.|[0027] Preferably, the gradient reaction tower 10 has a height of 4m, a diameter of 1: 1m, a height of 1.5: 1.5 m at the upper layer, a height of 1: 1m at the middle layer and a height of 1.5: 1.5 m at the lower layer, and a cone angle of 45-60 DEG in a conical structure at the bottom.|[0028] Preferably, the annular CO 2 distributor 6 is provided with nozzles in an annular distribution, the caliber of the nozzles is 0.1-0.5 mm, and the nozzles are arranged towards the second annular red mud distributor 5, so that CO 2 flowing in the annular CO 2 distributor 6 flows from the bottom end of the multi-layer micro-channel mixing module 9 towards the ultrasonic transducer 7.|[0029] Preferably, the pH of the feed solution obtained after step S1 is >10.|[0030] Preferably, the temperature of the drying tower is T1, the temperature of 100 ℃ is less than or equal to T1 and is less than 120 ℃, the dried red mud is crushed to 150-200 meshes by a ball mill 2, and the crushed red mud is mixed with deionized water according to a liquid-solid ratio of 8-10:1.|[0031] The supercritical CO 2 reaction pressure in the step S2 is P1, the pressure is adjusted to be absolute pressure, the supercritical CO 2 reaction temperature in the step S3 is T2,10MPa < P1 is less than or equal to 25MPa, and the temperature of 35 ℃ is less than or equal to 80 ℃.|[0032] Preferably, the ultrasonic crushing of S3 adopts a piezoelectric ceramic transducer with the frequency of 40 kHz, and the dynamic amplitude regulation and control range is 10-100%, so that the particle size of the red mud is reduced to 1-5 mu m.|[0033] Preferably, the porous supported catalyst of S4 is prepared by (1) synthesizing a carrier by using zinc acetate dihydrate, 2-methylimidazole and methanol by a sol-gel method. Dissolving 20 g zinc acetate dihydrate in 400mL of methanol to form a solution A, dissolving 30g of 2-methylimidazole in 400mL of methanol to obtain a solution B, rapidly mixing the solution A and the solution B, stirring the solution A and the solution B at 25 ℃ for 12 h, standing and ageing the solution A and the solution B for 24 h, centrifugally collecting white precipitate, washing the white precipitate with methanol for 3 times, and drying the white precipitate at 80 ℃ in an oven for 12 h to obtain carrier powder;| (2) Preparing an impregnating solution with the total molar mass of 1.5mol/L by using calcium nitrate and magnesium nitrate according to the molar ratio of Ca to Mg=2:1, and impregnating the carrier in the impregnating solution to obtain an impregnated carrier; | (3) And (3) placing the impregnated carrier in an N 2 atmosphere for gradient calcination, calcining at 100-150 ℃ for 1-2 hours to dehydrate, calcining at 300-400 ℃ for 2-3 hours to decompose nitrate to generate MgO/CaO nano-particles, calcining at 550-650 ℃ for 3-4 hours to form stable oxide in the impregnated carrier, and performing gas phase hydrophobic modification on the carrier to obtain the porous supported catalyst, wherein the water contact angle of the porous supported catalyst is more than 130 degrees, and the porous supported catalyst has strong hydrophobicity. |[0034] Preferably, in step S4, the multi-layer micro-channel mixing module 9 is formed by stacking multiple layers of titanium alloy micro-channel plates, and the single plate contains 800-4000 regular hexagonal flow channels with a butt edge distance of 50-300 μm.|[0035] Preferably, the addition amount of the porous supported catalyst added in the step S4 is 2-10wt% (calculated by the mass of the red mud) of the dry red mud powder.|[0036] S5, a baffle plate 12 is arranged in the gradient reaction tower 10, the material residence time is prolonged to 8-10 minutes, and the carbon fixation rate is more than or equal to 95%.|[0037] The working principle and the working process of the device are that firstly, the red mud is heated to 100-120 ℃ through a red mud drying tower 1, the red mud is dried, and then the dried red mud enters a ball mill 2 to be ground to 150-200 meshes; the pretreated red mud enters an ultrasonic crushing module through a red mud feeding pipe 16 and a first red mud annular distributor 4, and deionized water is introduced into a water inlet pipe 15; the method comprises the steps of carrying out ultrasonic crushing, feeding a porous supported catalyst into a multi-layer microchannel mixing module 9 through a catalyst feed pipe 14, carrying out pretreatment on red mud, pressurizing CO 2 to the pressure required by supercritical CO 2 in a multi-stage reciprocating compressor 11 while carrying out pretreatment on the red mud, uniformly distributing the material into the multi-layer microchannel mixing module 9 through a CO 2 annular distributor 6, carrying out three-phase instantaneous mixing on supercritical CO 2, red mud slurry and catalyst after the material is fed into the multi-layer microchannel mixing module 9, carrying out gradient temperature reaction on the mixed three-phase mixed slurry in a gradient reaction tower 10 through an ultrasonic-microchannel synergistic effect, reducing the particle size of the red mud to 1-5 mu m, completing three-phase mixing with supercritical CO 2 in 0.5 seconds, simultaneously adopting the porous supported calcium-magnesium composite catalyst, utilizing the limited domain effect and hydrophobicity of a carrier, improving the carbon fixation efficiency to be more than 95%, thoroughly solving the problem of silicate side reaction caused by over-strong alkalinity, starting a circulating pump 19 at intervals, pumping out the three-phase mixed slurry after mixing and feeding the three-phase mixed slurry into a gradient reaction tower 10 through a feed back pipe for a period of time, prolonging the corrosion life of the red mud, and prolonging the corrosion of a device after the solid reaction, and reducing the corrosion life of the device, cooling, and continuously treating the new red mud and CO 2 in the red mud drying tower 1, the ball mill 2 and the multistage reciprocating compressor 11 when the reactor works, so that the whole process is continuous.|[0038] The invention is further illustrated below with reference to examples.|[0039] Example 1|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 105 ℃ for 24 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 150-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=12 MPa; | s3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 60 percent), and the particle size of the red mud is crushed to 4 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.4 seconds; | S5, reacting the mixed materials in a gradient reaction tower 10 (the upper layer is at 38 ℃ per the middle layer is at 55 ℃ per the lower layer is at 70 ℃), adding 5 wt% of porous supported catalyst, and reacting for 8min; | After the reaction is finished, acidolysis-gas chromatography (acidolysis: the reacted red mud sample is filtered through a 200-mesh sieve to react with hydrochloric acid and is oscillated, and CO2 generated by the reaction is collected for gas chromatography analysis and quantitative calculation) is adopted to measure the carbon fixation efficiency, and the carbon fixation rate is 94.7%. |[0040] Example 2|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 110 ℃ for 26 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 200-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=18 MPa; | S3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 80%) and the particle size of the red mud is crushed to 2 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.3 seconds; | S5, reacting the mixed materials in a gradient reaction tower 10 (the upper layer is 42 ℃ per the middle layer is 58 ℃ per the lower layer is 75 ℃), and adding 8 wt% of porous supported catalyst for 9min; | after the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 96.2%. |[0041] Example 3|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 100 ℃ for 26 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 200-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=22 MPa; | S3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 70 percent), and the particle size of the red mud is crushed to 1.5 mu m; | s4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.5 seconds; | S5, reacting the mixed material in a gradient reaction tower 10 (the upper layer is 45 ℃ or the middle layer is 62 ℃ or the lower layer is 78 ℃), adding 3 wt% of porous supported catalyst, and reacting for 10min; | After the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 95.1%. |[0042] Example 4|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 115 ℃ for 18 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 160-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=15 MPa; | S3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 50%) and the particle size of the red mud is crushed to 4 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module, wherein the mixing time is 0.6 seconds; | s5, reacting the mixed material in a gradient reaction tower 10 (the upper layer is 35 ℃ per the middle layer is 50 ℃ per the lower layer is 65 ℃), adding 10 wt% of porous supported catalyst, and reacting for 8.5min; | after the reaction is completed, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 94.3%. |[0043] Example 5|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 108 ℃ for 22 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 170-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=25 MPa; | s3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 90 percent), and the particle size of the red mud is crushed to 1 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.2 seconds; | S5, reacting the mixed material in a gradient reaction tower 10 (the upper layer is 48 ℃ and the middle layer is 65 ℃ and the lower layer is 80 ℃), adding 2 wt% of porous supported catalyst, and reacting for 9.5min; | after the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, the carbon fixation rate is 96.8 percent, |Example 6|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 112 ℃ for 20 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 190-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=10 MPa; | s3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 75%) and the particle size of the red mud is crushed to 5 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module, wherein the mixing time is 0.7 seconds; | S5, reacting the mixed materials in a gradient reaction tower 10 (the upper layer is 40 ℃ per the middle layer is 55 ℃ per the lower layer is 70 ℃), adding 6 wt% of porous supported catalyst, reacting for 10min, and the return material proportion of a circulating pump 19 group is 15%; | After the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 95.9%. |[0044] Example 7|S1, taking Bayer process red mud, cleaning the red mud, drying the red mud at 105 ℃ for 24 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 150-mesh sieve;| S2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=20 MPa; | s3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 85 percent), and the particle size of the red mud is crushed to 2.5 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.4 seconds; | S5, the mixture is reacted in a gradient reaction tower 10 (the upper layer is 50 ℃ and the middle layer is 65 ℃ and the lower layer is 80 ℃), 7 wt% porous supported catalyst is added, and the reaction time is 8min. |After the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 95.3%.|[0045] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention. (CN120903536)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of red mud carbon fixation, in particular to a method and a device for realizing red mud carbon fixation under supercritical conditions.|BACKGROUND ART|[0002] Red mud is an industrial solid waste produced in the alumina production process. It has the characteristics of strong alkalinity, heavy metal content, high viscosity, fine granularity and the like. Long-term storage only occupies a large amount of land, and also can pollute water and soil. Therefore, a large amount of red mud is a solid waste which is needed to be treated and is urgently needed to be recycled, and the red mud is used as industrial solid waste with extremely high yield, and the problems of high carbon emission, potential resource waste of the red mud and the like exist in the traditional landfill, stockpiling or neutralization method. The supercritical CO 2 technology generates stable carbonate by reacting supercritical CO 2 with alkaline components in red mud, achieves the aim of 'carbon fixation by waste', and has the advantages of carbon sequestration and red mud harmless utilization.|DISCLOSURE|Disclosure of Invention|[0003] The invention mainly aims to provide a method and a device for realizing carbon fixation of red mud under supercritical conditions, which are used for solving the problem of red mud recycling treatment.|[0004] In order to achieve the above purpose, the invention provides a method for realizing carbon fixation of red mud under supercritical conditions, which comprises the following steps:| S1, cleaning red mud, drying to remove free moisture, crushing the dried red mud to form dried red mud powder, and mixing the dried red mud powder with deionized water in proportion; | S2, pressurizing CO 2 to supercritical pressure and supercritical temperature; | s3, ultrasonically crushing the slurry obtained in the step S1, and carrying out cavitation crushing through an ultrasonic array to reduce the particle size of the red mud; | S4, the crushed slurry, the pressurized supercritical CO 2 in the step S2 and the porous supported catalyst are mixed in a honeycomb microchannel in a three-phase manner, wherein the mixing time is less than or equal to 0.5 seconds; | s5, the mixed materials enter a gradient reaction tower, and are subjected to carbon fixation reaction under the condition of sectional temperature control and then cooled. |[0005] As a further improvement of the invention, in the step S1, the drying temperature is T1, the temperature is 100 ℃ less than or equal to T1 and less than 120 ℃, the dried red mud is crushed to 150-200 meshes, and the crushed red mud is mixed with deionized water according to a liquid-solid ratio of 8-10:1.|[0006] As a further improvement of the invention, the supercritical CO 2 reaction pressure in the step S2 is P1,10MPa < P1 is less than or equal to 25MPa, and the supercritical CO 2 reaction temperature in the step S3 is T2, wherein the temperature of 35 ℃ is less than or equal to 80 ℃.|[0007] As a further improvement of the invention, in the step S3, the piezoelectric ceramic transducer with the frequency of 40 kHz is adopted for ultrasonic crushing, and the dynamic amplitude regulation and control range is 10-100%, so that the particle size of the red mud is reduced to 1-5 mu m.|[0008] As a further improvement of the invention, the addition amount of the porous supported catalyst added in the step S4 is 2-10wt% of the dry red mud powder.|[0009] As a further improvement of the present invention, the porous supported catalyst in step S4 is prepared by the steps of:| (1) The method comprises the steps of adopting a sol-gel method to synthesize a carrier by utilizing zinc acetate dihydrate, 2-methylimidazole and methanol, weighing 20 g zinc acetate dihydrate, dissolving in 400 mL methanol to form a solution A, weighing 30 g of 2-methylimidazole, dissolving in 400 mL methanol to obtain a solution B, rapidly mixing the solution A and the solution B, stirring 12 h at 25 ℃, standing and aging 24 h, centrifugally collecting white precipitate, washing the white precipitate with methanol for 3 times, and drying 12 h at 80 ℃ in an oven to obtain carrier powder; | (2) Preparing an impregnating solution with the total molar mass of 1.5mol/L by using calcium nitrate and magnesium nitrate according to the molar ratio of Ca to Mg=2:1, and impregnating the carrier in the impregnating solution to obtain an impregnated carrier; | (3) And (3) placing the impregnated carrier in an N 2 atmosphere for gradient calcination, calcining at 100-150 ℃ for 1-2 hours to dehydrate, calcining at 300-400 ℃ for 2-3 hours to decompose nitrate to generate MgO/CaO nano-particles, calcining at 550-650 ℃ for 3-4 hours to form stable oxide in the impregnated carrier, and performing gas phase hydrophobic modification on the carrier to obtain the porous supported catalyst, wherein the water contact angle of the porous supported catalyst is more than 130 degrees, and the porous supported catalyst has strong hydrophobicity. |[0010] As a further improvement of the invention, the honeycomb microchannel in the step S4 is a microchannel mixing module, and is formed by stacking a plurality of layers of titanium alloy microchannel plates, and the single plate comprises 800-4000 regular hexagon flow channels with the opposite side distance of 50-300 mu m.|[0011] As a further improvement of the invention, in the step S5, the temperature of the upper low temperature region of the gradient reaction tower is 35-50 ℃, carbonate crystal nucleus is generated, the temperature of the middle temperature region is 50-65 ℃, crystal growth is promoted, and the temperature of the lower high temperature region is 65-80 ℃, and deep carbonization is carried out.|[0012] The device comprises a red mud drying tower, a ball mill communicated with the red mud drying tower, and a mixing outer cylinder arranged at an outlet of the ball mill, wherein a first red mud annular distributor, a second red mud annular distributor and a CO 2 annular distributor are arranged in the mixing outer cylinder from top to bottom, an ultrasonic transducer and a titanium alloy amplitude transformer are vertically arranged between the first red mud annular distributor and the second red mud annular distributor, a multi-layer microchannel mixing module is arranged between the second red mud annular distributor and the CO 2 annular distributor, a gradient reaction tower is arranged below the CO 2 annular distributor, a multi-stage reciprocating compressor is connected outside the CO 2 annular distributor, a plurality of groups of baffle plates are arranged in the gradient reaction tower at intervals, a pressure relief valve is arranged on the outer wall of the gradient reaction tower, a catalyst feed pipe is arranged at the top end of the gradient reaction tower, a water inlet pipe and a red mud feed pipe communicated with the ball mill are arranged on the first red mud annular distributor, a temperature and pressure control system is arranged outside the gradient reaction tower, a conical collector is arranged at the bottom end of the gradient reaction tower, a circulating pump is connected outside the conical collector, and the top of the gradient reaction tower is communicated with the circulating pump.|[0013] As a further improvement of the invention, the CO 2 annular distributor is annularly distributed with nozzles with the caliber of 0.1-0.5 mm, and the nozzles are arranged towards the second red mud annular distributor so that CO 2 flowing in the CO 2 annular distributor flows from the bottom end of the multi-layer micro-channel mixing module towards the ultrasonic transducer.|[0014] The beneficial effects of the invention are as follows:| 1. The invention can ensure that CO 2 maintains high diffusivity of gas under the condition of supercritical CO 2, simultaneously obtains strong dissolving capacity of liquid, has chemical inertness and mildness, can fully diffuse, fully contact with red mud, react with pore water or alkaline components in the red mud to generate carbonate ions, dissolve alkaline metal oxides (such as CaO) in the red mud to generate corresponding hydroxides, release soluble divalent metal ions (such as Mg 2+、Ca2+), and react with the carbonate ions to generate carbonate precipitates. The process not only can realize the aim of fixing carbon in the red mud, but also can reduce the alkalinity of the red mud, and is ready for the subsequent comprehensive utilization of the red mud. |[0015] 2. The invention only uses a supercritical CO 2 system, and does not use supercritical water and supercritical CO 2 to be applied in a combined way, but adopts a mode of adding a porous supported calcium-magnesium composite catalyst. The elimination of supercritical water can reduce the energy consumption of the whole reaction, and the water needs to reach a high temperature and a high pressure of >374 ℃ and >22.1MPa to reach a supercritical state, so that the whole reaction can be realized under milder conditions by using only supercritical CO 2. Titanate and silicate existing in the red mud compete with carbonate ions for soluble divalent cations (such as Ca 2+、Mg2+) in the red mud, which can be used for generating carbonate precipitation, so that the porous supported calcium-magnesium composite catalyst is added during the reaction, the competition between the titanate and silicate in the red mud is reduced, and the carbonate precipitation is easier to generate and the carbon fixing efficiency is higher. Meanwhile, compared with the prior art, the single calcium-based catalyst is used, the local pH is too high due to the too strong alkalinity, and silicate side reaction is initiated (silicate reacts with alkaline substances to generate silicate complex, alkaline substances are consumed, so that carbonate generation is reduced, and carbon fixing efficiency is affected). The alkaline (pH is about 10.3) of MgO is slightly lower than that of CaO (pH is about 12.5), and the pH is regulated and controlled by adding the magnesium-based catalyst, so that the generation of byproducts is reduced, and the carbon fixing efficiency is improved by more than 20%. In addition, mgO is more stable in a supercritical CO 2 environment, the combination capability of Mg 2+ and CO 32+ is stronger, and more stable MgCO 3 precipitate can be generated, so that the carbon fixing effect is better.|[0016] 3. The porous supported calcium-magnesium composite catalyst used in the invention is prepared by a sol-gel method, and a carrier is synthesized by zinc acetate dihydrate, 2-methylimidazole and methanol. Dissolving 20 g zinc acetate dihydrate in 400mL of methanol to form a solution A, dissolving 30 g of 2-methylimidazole in 400mL of methanol to obtain a solution B, rapidly mixing the solution A and the solution B, stirring the solution B at 25 ℃ for 12h, standing and aging the solution B for 24h, centrifugally collecting white precipitate, washing the white precipitate with methanol for 3 times, drying the white precipitate at 80 ℃ in an oven for 12h to obtain carrier powder, preparing calcium nitrate and magnesium nitrate into 1.5mol/L impregnating solution according to the molar ratio of Ca to Mg=2:1, loading the impregnating solution in an equal volume, calcining the impregnating solution in a gradient manner at 120 ℃,350 ℃ and 600 ℃ under the atmosphere of N 2, calcining the solution B at 120 ℃ for 2h to dehydrate the impregnating solution, calcining the solution B at 350 ℃ for 3h to decompose nitrate to generate MgO/CaO nano particles, calcining the red mud at 600 ℃ for 4h to form stable oxide, and finally performing gas phase hydrophobic modification on the hexamethyldisilazane to enable the water contact angle to be more than 130 ℃, so that the carrier powder has strong hydrophobicity, and prevents corrosion in the slurry and prevents catalyst from being deactivated.|[0017] 4. The porous supported calcium-magnesium composite catalyst used in the invention has a carrier pore canal of only 1.2nm, and limits CaO/MgO active components to nano-scale to form a high-density catalytic microreactor, so that the diffusion distance of CO 2 is shortened to nano-scale, and the carbon fixation rate is greatly improved. In addition, since silicate diameters are generally greater than 1.5nm, it is blocked by the support pore channels and eliminates competing side reactions.|[0018] 5. The reactor of the device adopts the combination of ultrasonic crushing, micro-channel mixing and gradient reaction towers, the reaction takes more than 30 minutes and the carbon fixation rate is only 89.5 percent due to uneven stirring in the traditional method, the device crushes red mud to the level of 1-5 mu m through 40 kHz ultrasonic cavitation, the mass transfer efficiency is improved by 60 times by combining with supercritical CO 2 turbulence in a honeycomb micro-channel, the reaction time is shortened to be within 10 minutes, and meanwhile, the three-section gradient temperature control reaction towers (35-80 ℃ accurate partition) cooperate with a catalyst with the finite field effect, so that the carbon fixation rate is improved to 95.5 percent, the ton red mud treatment energy consumption is only 120 kWh, and the traditional device is up to 200 kWh and has serious side reaction.|DRAWINGS DESCRIPTION|[0019] FIG. 1 is a schematic diagram of an apparatus used in the method for implementing carbon fixation of red mud under supercritical conditions;| Reference numerals illustrate: | 1. the device comprises a red mud drying tower, a ball mill, a3, a mixing outer cylinder, a 4, a first red mud annular distributor, a 5, a second red mud annular distributor, a 6, CO 2 annular distributor, a 7, an ultrasonic transducer, an 8, titanium alloy amplitude transformer, a 9, a multi-layer microchannel mixing module, a 10, a gradient reaction tower, a 11, a multi-stage reciprocating compressor, a 12, a baffle plate, a 13, a pressure relief valve, a 14, a catalyst feeding pipe, a 15, a water inlet pipe, a 16, a red mud feeding pipe, a 17, a temperature and pressure control system, a 18, a conical collector, a 19, a circulating pump, a 20 and a cooling water jacket. |INVENTION MODE|Detailed Description|[0020] The present application will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present application more apparent. It should be understood that the described embodiments are merely some, but not all embodiments of the present application. Embodiments of the application and features of the embodiments may be combined with each other without conflict. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to be within the scope of the application.|[0021] The invention discloses a method for realizing carbon fixation of red mud under supercritical conditions, which comprises the following steps:| S1, cleaning red mud, sending the red mud into a drying tower to remove free moisture, crushing the dried red mud by a ball mill 2 to form dried red mud powder, and mixing the dried red mud powder with deionized water in proportion; | S2, pressurizing CO 2 to supercritical pressure and supercritical temperature in a compressor; | S3, sending the slurry obtained in the step S1 into an ultrasonic crushing area, and carrying out cavitation crushing through an ultrasonic array to reduce the particle size of the red mud; | S4, enabling crushed slurry, pressurized supercritical CO 2 in the step S2 and the porous supported catalyst to enter a micro-channel mixing module in parallel, and completing three-phase mixing in a honeycomb micro-channel, wherein the mixing time is less than or equal to 0.5 seconds; | S5, the mixed materials enter a gradient reaction tower 10, carbon fixation reaction is carried out under the condition of sectional temperature control, and the temperature is reduced after the reaction is carried out for 10 min. |[0022] In order to ensure that supercritical CO 2, porous supported catalyst and crushed slurry are fully contacted, referring to fig. 1, the device further comprises a red mud drying tower 1, a ball mill 2 communicated with the red mud drying tower 1, a mixing outer cylinder 3 arranged at an outlet of the ball mill 2, a first red mud annular distributor 4, a second red mud annular distributor 5 and a CO 2 annular distributor 6 are arranged in the mixing outer cylinder 3 from top to bottom, an ultrasonic transducer 7 and a titanium alloy amplitude transformer 8 are vertically arranged between the first red mud annular distributor 4 and the second red mud annular distributor 5, a multi-layer micro-channel mixing module 9 is arranged between the second red mud annular distributor 5 and the CO 2 annular distributor 6, a gradient reaction tower 10 is arranged below the CO 2 annular distributor 6, a multistage reciprocating compressor 11 is connected to the outside of the CO 2 annular distributor 6, a plurality of groups of baffle plates 12 are arranged in the gradient reaction tower 10 at intervals, a pressure relief valve 13 is arranged on the outer wall of the gradient reaction tower 10, a catalyst feed pipe 14 is arranged at the top end of the gradient reaction tower 10, a feed pipe 16 is vertically arranged between the first annular distributor 4 and the second red mud annular distributor 5, a temperature control system 17 is arranged outside the gradient reaction tower 10, a conical collector 18 is arranged at the bottom of the gradient reaction tower 10, and a gradient circulation pump 19 is connected to the top of the gradient reaction tower 18 is connected to the gradient circulation pump 19.|[0023] The device comprises a red mud drying tower 1, a ball mill 2, a red mud feeding pipe 16, a water inlet pipe 15, a first red mud annular distributor 4, a second red mud annular distributor 5, an ultrasonic transducer 7, a titanium alloy amplitude transformer 8, a catalyst feeding pipe 14, a multi-layer micro-channel mixing module 9, a CO 2 annular distributor 6, a gradient reaction tower 10, a baffle plate 12, a multi-stage reciprocating compressor 11, a pressure relief valve 13, a temperature and pressure control system 17, a circulating pump 19, a cooling water jacket 20 and a conical collector 18, wherein the ultrasonic transducer 7 and the titanium alloy amplitude transformer 8 are arranged in a closed tubular structure and are vertically arranged, the upper end of the ultrasonic transducer is provided with the red mud feeding pipe 16 and the water inlet pipe 15, the two pipes are respectively fed with dried and crushed red mud and deionized water, the dried and crushed red mud are mixed and enter the first red mud annular distributor 4 to ensure that red mud slurry uniformly enters an ultrasonic crushing stage, the red mud slurry after ultrasonic crushing passes through a second red mud annular distributor 5 arranged at the lower end and then uniformly enters a multi-layer micro-channel mixing module 9, the multi-layer micro-channel mixing module 9 is arranged in a closed tubular structure, the multi-layer micro-channel mixing module 9 is connected with the ultrasonic crushing module through the second red mud annular distributor 5, a catalyst feeding pipe 14 is arranged at the upper end, a CO 2 annular distributor 6 is arranged at the lower end, a catalyst and supercritical CO 2 respectively enter the multi-layer micro-channel mixing module 9 from the two ends, three phases are instantaneously mixed through micro-channels, the mixed slurry enters a gradient reaction tower 10 connected below the multi-layer micro-channel mixing module 9, carbonate crystal nuclei are generated in an upper low temperature region (35-50 ℃) of the gradient reaction tower 10, crystal growth is promoted in a middle medium temperature region (50-65 ℃) and deep carbonization is completed in a lower high temperature region (65-80 ℃), the temperature is controlled by a temperature pressure control system 17. The baffle plates 12 are arranged in the gradient reaction tower 10, and 8-10 pieces are arranged from top to bottom. The pressure release valve 13 is used for releasing pressure when the reaction pressure is exceeded to ensure safety, and the multistage reciprocating compressor 11 is used for pressurizing CO 2 to supercritical CO 2 reaction pressure and then uniformly inputting the CO 2 reaction pressure into the multilayer microchannel mixing module 9 through the CO 2 annular distributor 6.|[0024] Preferably, the outer layer of the ultrasonic crushing module is provided with a cooling water jacket 20 to prevent the temperature from being too high during ultrasonic treatment.|[0025] Preferably, the ultrasonic crushing module has a height of 1.5 m, a diameter of 1m, an ultrasonic transducer 7 diameter of 300 mm, a length of 200 mm (including a horn), a cooling water jacket 20 wall thickness of 2 mm and a sandwich inner diameter of 8 mm.|[0026] Preferably, the multilayer microchannel mixing module 9 has a height of 1.8 m and a diameter of 1. 1m, and a single-layer microchannel plate thickness of 100. 100 mm and a diameter of 0.98 m.|[0027] Preferably, the gradient reaction tower 10 has a height of 4m, a diameter of 1: 1m, a height of 1.5: 1.5 m at the upper layer, a height of 1: 1m at the middle layer and a height of 1.5: 1.5 m at the lower layer, and a cone angle of 45-60 DEG in a conical structure at the bottom.|[0028] Preferably, the annular CO 2 distributor 6 is provided with nozzles in an annular distribution, the caliber of the nozzles is 0.1-0.5 mm, and the nozzles are arranged towards the second annular red mud distributor 5, so that CO 2 flowing in the annular CO 2 distributor 6 flows from the bottom end of the multi-layer micro-channel mixing module 9 towards the ultrasonic transducer 7.|[0029] Preferably, the pH of the feed solution obtained after step S1 is >10.|[0030] Preferably, the temperature of the drying tower is T1, the temperature of 100 ℃ is less than or equal to T1 and is less than 120 ℃, the dried red mud is crushed to 150-200 meshes by a ball mill 2, and the crushed red mud is mixed with deionized water according to a liquid-solid ratio of 8-10:1.|[0031] The supercritical CO 2 reaction pressure in the step S2 is P1, the pressure is adjusted to be absolute pressure, the supercritical CO 2 reaction temperature in the step S3 is T2,10MPa < P1 is less than or equal to 25MPa, and the temperature of 35 ℃ is less than or equal to 80 ℃.|[0032] Preferably, the ultrasonic crushing of S3 adopts a piezoelectric ceramic transducer with the frequency of 40 kHz, and the dynamic amplitude regulation and control range is 10-100%, so that the particle size of the red mud is reduced to 1-5 mu m.|[0033] Preferably, the porous supported catalyst of S4 is prepared by (1) synthesizing a carrier by using zinc acetate dihydrate, 2-methylimidazole and methanol by a sol-gel method. Dissolving 20 g zinc acetate dihydrate in 400mL of methanol to form a solution A, dissolving 30g of 2-methylimidazole in 400mL of methanol to obtain a solution B, rapidly mixing the solution A and the solution B, stirring the solution A and the solution B at 25 ℃ for 12 h, standing and ageing the solution A and the solution B for 24 h, centrifugally collecting white precipitate, washing the white precipitate with methanol for 3 times, and drying the white precipitate at 80 ℃ in an oven for 12 h to obtain carrier powder;| (2) Preparing an impregnating solution with the total molar mass of 1.5mol/L by using calcium nitrate and magnesium nitrate according to the molar ratio of Ca to Mg=2:1, and impregnating the carrier in the impregnating solution to obtain an impregnated carrier; | (3) And (3) placing the impregnated carrier in an N 2 atmosphere for gradient calcination, calcining at 100-150 ℃ for 1-2 hours to dehydrate, calcining at 300-400 ℃ for 2-3 hours to decompose nitrate to generate MgO/CaO nano-particles, calcining at 550-650 ℃ for 3-4 hours to form stable oxide in the impregnated carrier, and performing gas phase hydrophobic modification on the carrier to obtain the porous supported catalyst, wherein the water contact angle of the porous supported catalyst is more than 130 degrees, and the porous supported catalyst has strong hydrophobicity. |[0034] Preferably, in step S4, the multi-layer micro-channel mixing module 9 is formed by stacking multiple layers of titanium alloy micro-channel plates, and the single plate contains 800-4000 regular hexagonal flow channels with a butt edge distance of 50-300 μm.|[0035] Preferably, the addition amount of the porous supported catalyst added in the step S4 is 2-10wt% (calculated by the mass of the red mud) of the dry red mud powder.|[0036] S5, a baffle plate 12 is arranged in the gradient reaction tower 10, the material residence time is prolonged to 8-10 minutes, and the carbon fixation rate is more than or equal to 95%.|[0037] The working principle and the working process of the device are that firstly, the red mud is heated to 100-120 ℃ through a red mud drying tower 1, the red mud is dried, and then the dried red mud enters a ball mill 2 to be ground to 150-200 meshes; the pretreated red mud enters an ultrasonic crushing module through a red mud feeding pipe 16 and a first red mud annular distributor 4, and deionized water is introduced into a water inlet pipe 15; the method comprises the steps of carrying out ultrasonic crushing, feeding a porous supported catalyst into a multi-layer microchannel mixing module 9 through a catalyst feed pipe 14, carrying out pretreatment on red mud, pressurizing CO 2 to the pressure required by supercritical CO 2 in a multi-stage reciprocating compressor 11 while carrying out pretreatment on the red mud, uniformly distributing the material into the multi-layer microchannel mixing module 9 through a CO 2 annular distributor 6, carrying out three-phase instantaneous mixing on supercritical CO 2, red mud slurry and catalyst after the material is fed into the multi-layer microchannel mixing module 9, carrying out gradient temperature reaction on the mixed three-phase mixed slurry in a gradient reaction tower 10 through an ultrasonic-microchannel synergistic effect, reducing the particle size of the red mud to 1-5 mu m, completing three-phase mixing with supercritical CO 2 in 0.5 seconds, simultaneously adopting the porous supported calcium-magnesium composite catalyst, utilizing the limited domain effect and hydrophobicity of a carrier, improving the carbon fixation efficiency to be more than 95%, thoroughly solving the problem of silicate side reaction caused by over-strong alkalinity, starting a circulating pump 19 at intervals, pumping out the three-phase mixed slurry after mixing and feeding the three-phase mixed slurry into a gradient reaction tower 10 through a feed back pipe for a period of time, prolonging the corrosion life of the red mud, and prolonging the corrosion of a device after the solid reaction, and reducing the corrosion life of the device, cooling, and continuously treating the new red mud and CO 2 in the red mud drying tower 1, the ball mill 2 and the multistage reciprocating compressor 11 when the reactor works, so that the whole process is continuous.|[0038] The invention is further illustrated below with reference to examples.|[0039] Example 1|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 105 ℃ for 24 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 150-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=12 MPa; | s3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 60 percent), and the particle size of the red mud is crushed to 4 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.4 seconds; | S5, reacting the mixed materials in a gradient reaction tower 10 (the upper layer is at 38 ℃ per the middle layer is at 55 ℃ per the lower layer is at 70 ℃), adding 5 wt% of porous supported catalyst, and reacting for 8min; | After the reaction is finished, acidolysis-gas chromatography (acidolysis: the reacted red mud sample is filtered through a 200-mesh sieve to react with hydrochloric acid and is oscillated, and CO2 generated by the reaction is collected for gas chromatography analysis and quantitative calculation) is adopted to measure the carbon fixation efficiency, and the carbon fixation rate is 94.7%. |[0040] Example 2|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 110 ℃ for 26 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 200-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=18 MPa; | S3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 80%) and the particle size of the red mud is crushed to 2 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.3 seconds; | S5, reacting the mixed materials in a gradient reaction tower 10 (the upper layer is 42 ℃ per the middle layer is 58 ℃ per the lower layer is 75 ℃), and adding 8 wt% of porous supported catalyst for 9min; | after the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 96.2%. |[0041] Example 3|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 100 ℃ for 26 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 200-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=22 MPa; | S3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 70 percent), and the particle size of the red mud is crushed to 1.5 mu m; | s4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.5 seconds; | S5, reacting the mixed material in a gradient reaction tower 10 (the upper layer is 45 ℃ or the middle layer is 62 ℃ or the lower layer is 78 ℃), adding 3 wt% of porous supported catalyst, and reacting for 10min; | After the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 95.1%. |[0042] Example 4|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 115 ℃ for 18 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 160-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=15 MPa; | S3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 50%) and the particle size of the red mud is crushed to 4 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module, wherein the mixing time is 0.6 seconds; | s5, reacting the mixed material in a gradient reaction tower 10 (the upper layer is 35 ℃ per the middle layer is 50 ℃ per the lower layer is 65 ℃), adding 10 wt% of porous supported catalyst, and reacting for 8.5min; | after the reaction is completed, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 94.3%. |[0043] Example 5|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 108 ℃ for 22 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 170-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=25 MPa; | s3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 90 percent), and the particle size of the red mud is crushed to 1 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.2 seconds; | S5, reacting the mixed material in a gradient reaction tower 10 (the upper layer is 48 ℃ and the middle layer is 65 ℃ and the lower layer is 80 ℃), adding 2 wt% of porous supported catalyst, and reacting for 9.5min; | after the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, the carbon fixation rate is 96.8 percent, |Example 6|S1, taking Bayer process red mud of an aluminum plant, cleaning the red mud, drying the red mud at 112 ℃ for 20 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 190-mesh sieve;| s2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=10 MPa; | s3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 75%) and the particle size of the red mud is crushed to 5 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module, wherein the mixing time is 0.7 seconds; | S5, reacting the mixed materials in a gradient reaction tower 10 (the upper layer is 40 ℃ per the middle layer is 55 ℃ per the lower layer is 70 ℃), adding 6 wt% of porous supported catalyst, reacting for 10min, and the return material proportion of a circulating pump 19 group is 15%; | After the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 95.9%. |[0044] Example 7|S1, taking Bayer process red mud, cleaning the red mud, drying the red mud at 105 ℃ for 24 hours, crushing the red mud by a ball mill 2, and sieving the red mud by a 150-mesh sieve;| S2, pressurizing CO 2 to supercritical CO 2 reaction pressure in the multistage reciprocating compressor 11, and adjusting absolute pressure P1=20 MPa; | s3, the slurry enters an ultrasonic crushing area (frequency 40 kHz, amplitude 85 percent), and the particle size of the red mud is crushed to 2.5 mu m; | S4, enabling the crushed slurry and the supercritical CO 2 to enter a multi-layer micro-channel mixing module 9, wherein the mixing time is 0.4 seconds; | S5, the mixture is reacted in a gradient reaction tower 10 (the upper layer is 50 ℃ and the middle layer is 65 ℃ and the lower layer is 80 ℃), 7 wt% porous supported catalyst is added, and the reaction time is 8min. |After the reaction is finished, the acidolysis-gas chromatography is adopted to determine the carbon fixation efficiency, and the carbon fixation rate is 95.3%.|[0045] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention. Family Number|(116599289)|116599289|Abstract|(CN120903536 A)|The invention discloses a method and a device for realizing red mud carbon sequestration under supercritical conditions , and relates to the technical field of red mud carbon sequestration , the method comprises a red mud pretreatment step , an ultrasonic cavitation crushing step and a microchannel mixing reaction step , the device comprises a pretreatment unit , an ultrasonic crushing module , a micro - channel mixing module , a gradient reaction tower , a temperature and pressure control system , a multi - stage reciprocating compressor and an external circulating pump . An ultrasonication area is arranged at the top , a honeycomb - shaped micro - channel mixing module is integrated in the middle , a gradient temperature reaction tower is arranged at the bottom , a baffle plate is arranged for strengthening mass transfer , and after a carbon sequestration reaction is completed , slurry returns to the reaction area through a circulating pump ; the particle size of the red mud is reduced to 1-5 [ mu ] m through the ultrasonic - microchannel synergistic effect , and three - phase mixing of the red mud and supercritical CO2 is completed within 0.5 s ; meanwhile , a porous supported calcium - magnesium composite catalyst is adopted , the confinement effect and hydrophobicity of a carrier are utilized , the carbon sequestration efficiency is improved to 95% or above , and the problem of silicate side reaction caused by too strong alkalinity is solved . |CPC codes|(CN120903536 A)|B01F - 033/30 |B01F - 033/831 |B01J - 008/02 |C01F - 007/06/6 |IPC codes|(CN120903536 A)|B01F - 033/30 |B01F - 033/83 |B01J - 008/02 |C01F - 007/066 |Title|(CN120903536 A)|Method and device for realizing carbon sequestration of red mud under supercritical condition | Chemical engineering|Materials, metallurgy B01F-003/04|B01F-003/04/51|B01F-005/04/73|B01F-005/04/8|B01F-005/06/4|B01F-005/06/47|B01F-007/00/775|B01F-013/00/59|B01F-2215/0431|B01J-008/00/85|B01J-008/04/53|B01J-008/04/92|B01J-008/04/96|B01J-012/00|B01J-019/00/93|B01J-019/24|B01J-019/24/05|B01J-019/24/5|B01J-019/24/9|B01J-020/28/014|B01J-020/281|B01J-2208/00362|B01J-2208/00849|B01J-2208/00938|B01J-2219/00177|B01J-2219/00768|B01J-2219/00783|B01J-2219/0086|B01J-2219/00889|B01J-2219/00916|B01J-2219/0884|B01J-2219/24|B01J-2219/2474|B01J-2219/2475|B01J-2220/82|B01L-003/502746|B01L-007/52|B82Y-040/00|C01B-003/36|C01B-032/19|C01B-2203/062|C01F-007/02|C01P-2002/72|C02F-2101/30|C07C-011/24|C07C-017/04|C07C-019/08|C08K-2003/2258|C10G-031/08|C10G-045/00|C10G-047/00|C10G-049/00/2|C10L-001/02|C10L-2290/24|C12M-027/24|G01N-030/60/69 B01F-003/04|B01F-003/04/51|B01F-005/04/73|B01F-005/04/8|B01F-005/06/4|B01F-005/06/47|B01F-007/00/775|B01F-013/00/59|B01F-2215/0431|B01J-008/00/85|B01J-008/04/53|B01J-008/04/92|B01J-008/04/96|B01J-012/00|B01J-019/00/93|B01J-019/24|B01J-019/24/05|B01J-019/24/5|B01J-019/24/9|B01J-020/28/014|B01J-020/281|B01J-2208/00362|B01J-2208/00849|B01J-2208/00938|B01J-2219/00177|B01J-2219/00768|B01J-2219/00783|B01J-2219/0086|B01J-2219/00889|B01J-2219/00916|B01J-2219/0884|B01J-2219/24|B01J-2219/2474|B01J-2219/2475|B01J-2220/82|B01L-003/502746|B01L-007/52|B82Y-040/00|C01B-003/36|C01B-032/19|C01B-2203/062|C01F-007/02|C01P-2002/72|C02F-2101/30|C07C-011/24|C07C-017/04|C07C-019/08|C08K-2003/2258|C10G-031/08|C10G-045/00|C10G-047/00|C10G-049/00/2|C10L-001/02|C10L-2290/24|C12M-027/24|G01N-030/60/69 B01F-033/30|B01F-033/83|B01J-008/02|C01F-007/066 B01F-033/30|B01F-033/83|B01J-008/02|C01F-007/066 PENDING (CN120903536)|PENDING ALIVE (CN120903536)|ALIVE (CN120903536)|LEGAL DETAILS FOR CN120903536|Actual or expected expiration date=2045-08-12|Legal state=ALIVE|Status=PENDING|Event publication date=2025-08-12|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511126466|Application date=2025-08-12|Standardized application number=2025CN-1126466|Event publication date=2025-11-07|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120903536|Publication stage code=A|Publication date=2025-11-07|Standardized publication number=CN120903536|Event publication date=2025-11-07|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-11-25|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN120903536)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKcVxxBzIQwwSFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000079615353&ekey=2090&xpn=CN120903536&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=fNr7Zx2NLJySXa87XAaKF5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN120903536)|CN (CN120903536)|NAME=KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN120903536)|NAME=WANG YUKUI;Kunming Longhe Intellectual Property Agency (General Partnership) , REG=53220 (CN120903536)|NAME=HUANG JIANHONG|NAME=JIANG ZHUOLUN|NAME=ZUO JIANFEN|NAME=LUO QIULI|NAME=ZHU BIN|NAME=XIE XIN|NAME=TIAN SENLIN|NAME=ZHAO QUN|NAME=LI JIE 0 1 Titre: (CN120903536)|Method and device for realizing carbon sequestration of red mud under supercritical condition Résumé: (CN120903536)|The invention discloses a method and a device for realizing red mud carbon sequestration under supercritical conditions, and relates to the technical field of red mud carbon sequestration, the method comprises a red mud pretreatment step, an ultrasonic cavitation crushing step and a microchannel mixing reaction step, the device comprises a pretreatment unit, an ultrasonic crushing module, a micro-channel mixing module, a gradient reaction tower, a temperature and pressure control system, a multi-stage reciprocating compressor and an external circulating pump. An ultrasonication area is arranged at the top, a honeycomb-shaped micro-channel mixing module is integrated in the middle, a gradient temperature reaction tower is arranged at the bottom, a baffle plate is arranged for strengthening mass transfer, and after a carbon sequestration reaction is completed, slurry returns to the reaction area through a circulating pump; the particle size of the red mud is reduced to 1-5 [mu] m through the ultrasonic-microchannel synergistic effect, and three-phase mixing of the red mud and supercritical CO2 is completed within 0.5 s; meanwhile, a porous supported calcium-magnesium composite catalyst is adopted, the confinement effect and hydrophobicity of a carrier are utilized, the carbon sequestration efficiency is improved to 95% or above, and the problem of silicate side reaction caused by too strong alkalinity is solved. 53 Abstract gpt-4o-mini no The focus is on carbon sequestration using red mud under supercritical conditions, which does not involve the accelerated weathering of silicate or alkaline minerals for CO₂ capture.
54 US11/064,756|US12/138,019 US12/138,019|CA2537383|US11/064,756 US9028607|CA2537383|US20080245274|US7390444|CA2537383|US20060185560 4099265 US9028607 B2 2015-05-12 [US9028607]|US20080245274 A1 2008-10-09 [US20080245274]|CA2537383 C 2012-04-17 [CA2537383]|CA2537383 A1 2006-08-24 [CA2537383]|US7390444 B2 2008-06-24 [US7390444]|US20060185560 A1 2006-08-24 [US20060185560] 2005-02-24|2008-06-12 2008-06-12|2006-02-21|2005-02-24 2015-05-12|2012-04-17|2008-10-09|2008-06-24|2006-08-24|2006-08-24 (US9028607)|2015-05-12|(US7390444)|2008-06-24|(CA2537383)|2012-04-17 (US9028607)|2023-06-19|(US7390444)|2020-07-27|(CA2537383)|2020-02-21 (US9028607)|Carbon dioxide sequestration in foamed controlled low strength materials (US9028607)|A process for sequestering carbon dioxide from the exhaust gas emitted from a combustion chamber is disclosed. In the process, a foam including a foaming agent and the exhaust gas is formed, and the foam is added to a mixture including a cementitious material (e.g., cement-kiln dust, lime kiln dust, or slag cement) and water to form a foamed mixture. Thereafter, the foamed mixture is allowed to set, preferably to a controlled low-strength material having a compressive strength of 1200 psi or less. The carbon dioxide in the exhaust gas reacts with hydration products in the controlled low-strength material and in turn sequesters the carbon dioxide. WISCONSIN ELECTRIC POWER (US9028607)|Wisconsin Electric Power Company ([US])|(US20080245274)|RAMME BRUCE W|(US7390444)|Wisconsin Electric Power Company ([US])|(US20060185560)|Wisconsin Electric Power Company|(CA2537383)|WISCONSIN ELECTRIC POWER COMPANY ([US])|(CA2537383)|WISCONSIN ELECTRIC POWER COMPANY ([US]) RAMME BRUCE W (US9028607)|Ramme Bruce W.|(US20080245274)|Ramme Bruce W. (US9028607)|Quarles & Brady LLP|(US7390444)|Quarles & Brady LLP|(CA2537383)|LAVERY, DE BILLY, LLP ([CA]) (US9028607)|Also advantageously, the man made carbon dioxide emissions from a fossil fuel burning plant are decreased by sequestration of the carbon dioxide in the foamed controlled low-strength material.|The use of cement-kiln dust, lime-kiln dust, and/or slag cement in CLSM provides a environmentally beneficial use for these cementitious materials.|There is a continuing need to safely and economically dispose of such industrial by-products as cement-kiln dust, lime-kiln dust, and slag cement; thus, there is a continuing need for products and processes that make environmentally beneficial use of these by-products.|Maintaining cement-kiln dust landfills is expensive and difficult because of the fine, dusty nature of the material, and disposal costs add significantly to the cost of cement manufacture.| (US9028607)|1. A process for preparing a controlled low-strength material having a compressive strength of 1200 psi or less, the process comprising: preparing a mixture including water and a cementitious material, wherein the cementitious material is selected from the group consisting of cement-kiln dust, lime-kiln dust, and slag cement; recovering exhaust gas from a combustion chamber, wherein the exhaust gas includes carbon dioxide; forming a foam including a foaming agent and the exhaust gas; mixing the foam into the mixture to form a foamed mixture; and thereafter allowing the foamed mixture to set to form the controlled low-strength material, wherein during the step of allowing the foamed mixture to set, the carbon dioxide in the exhaust gas reacts with hydration products in the controlled low-strength material to sequester carbon dioxide.|18. A process for sequestering carbon dioxide from exhaust gas emitted from a combustion chamber, the process comprising: forming a foam including a foaming agent and the exhaust gas; mixing the foam with a mixture including a cementitious material, wherein the cementitious material is selected from the group consisting of cement-kiln dust, lime-kiln dust, and slag cement, to form a foamed mixture; and allowing the foamed mixture to set, wherein the mixture sets to a controlled low-strength material having a compressive strength of 1200 psi or less, and wherein during the step of allowing the foamed mixture to set, the carbon dioxide in the exhaust gas reacts with hydration products in the controlled low-strength material to sequester carbon dioxide.|22. A process for sequestering carbon dioxide from a gas including one weight percent or more carbon dioxide, the process comprising: forming a foam including a foaming agent and the gas; mixing the foam with a mixture including water and a material selected from the group consisting of cement-kiln dust, lime-kiln dust, and slag cement, to form a foamed mixture; and allowing the foamed mixture to set to a controlled low-strength material having a compressive strength of 1200 psi or less, wherein during the step of allowing the foamed mixture to set, the carbon dioxide in the exhaust gas reacts with hydration products in the controlled low-strength material to sequester carbon dioxide.| (US9028607)|The invention relates to a process for sequestering carbon dioxide through the production of lightweight controlled low-strength materials.|This invention relates to a process for sequestering carbon dioxide through the production of lightweight controlled low-strength materials.|Thus, the invention provides products and processes that make environmentally beneficial use of the carbon dioxide produced as by-products of the combustion of fossil fuels in the combustion chambers of power and industrial production plants, the cement-kiln dust produced as a by-product of portland cement production, the lime-kiln dust produced as a by-product of lime production, and the slag cement produced as a by-product of iron and steel production.| (US9028607)|CONTROLLED LOW STRENGTH MATERIAL(100,95)|METHANEDIONE(100,59)|PSI(100,49)|COMPRESSIVE STRENGTH(100,30)|GAS(100,25)|EXHAUST GAS(100,15)|COMBUSTION CHAMBER(100,9)|METHANEDIONE SEQUESTRATION(100,1)|HYDRATION PRODUCT(39,7)|CEMENT KILN DUST(38,128)|LIME KILN DUST(38,126)|FOAM(35,51)|SLAG CEMENT(34,29)|CEMENTITIOUS MATERIAL(33,22)|CUBIC YARD(28,15)|FOAMING AGENT EXPANSION(28,3)|PORTLAND CEMENT PRODUCTION(24,1)|LIME PRODUCTION(22,1)|COMPRESSOR(19,5)|ANNUAL SEQUESTRATION ESTIMATE ASSUMPTION(19,3)|EXHAUST GAS COMPRESSION(19,3)|FOAMING AGENT(18,17)|INDUSTRIAL PRODUCTION PLANT(13,2)|PELLETIZING(13,1)|CUBIC FOOT(12,6)|METHANEDIONE PERMANENT SEQUESTRATION(12,2)|POWER COMBUSTION CHAMBER(12,1)|MOL CO2(11,12)|METHANEDIONE OCEAN SEQUESTRATION(11,1)|MOLTEN SLAG(10,5)|FOSSIL FUEL(9,6)|MOL NA2O(9,6)|MONTH AGE(9,5)|METHANEDIONE EMISSION(9,3)|SHAPING(9,2)|CARBONATION REACTION(8,4)|CARBONATION TESTING(8,3)|GRAVIMETRIC TESTING(8,3)|METHANEDIONE FOAM(8,2)|MULTICOMPONENT GAS STREAM(8,2)|AMERICAN CONCRETE INSTITUTE COMMITTEE(8,1)|LIME BLAST KILN(8,1)|PUMICE LIGHTWEIGHT AGGREGATE(8,1)|STEEL PRODUCTION(8,1)|WEIGHT PERCENT(8,1)|AL2O3(7,23)|MOL CALCIUM HYDROXIDE(7,9)|CO2 LB(7,6)|MOL K2O(7,6)|MOL KOH(7,6)|CO2 TON(7,3)|MOL MAGNESIA(7,3)|RAW INGREDIENT(7,3)|SEVEN DAY AGE(7,3)|CO2 PERMANENT SEQUESTRATION(7,1)|CRUSHED GRAVEL AGGREGATE(7,1)|DOLOMITIC LIME KILN DUST(7,1)|FOAMED MORTAR BATCH(7,1)|AMERICAN SOCIETY(6,2)|ELASTIZELL CORPORATION(6,2)|MINERAL AGGREGATE(6,2)|OUTDOOR STORAGE PILE(6,2)|PHENOLPHTHALEIN INDICATOR TEST(6,2)|SUMMER SEASON(6,2)|BOREAL WETLAND(6,1)|CEMENT KILN DUST TON(6,1)|CONCRETE NATURAL CARBONATION(6,1)|DEEP SALINE AQUIFER(6,1)|GRAVITY MODULUS STAINING(6,1)|PARTICLE SIZE FRACTION(6,1)|UNDERSIZE FINE AGGREGATE FRACTION(6,1)|WESTERN LIME CORPORATION(6,1)|FLY ASH(5,10)|MOL MG(5,6)|PERCENT CO2(5,4)|CURED CYLINDER(5,3)|CURING STATION(5,3)|EARLY AGE(5,3)|CARBONATION DIFFERENCE(5,2)|FIVE GALLON PAIL(5,2)|LATE AGE(5,2)|THERMOGRAVIMETRIC ANALYSIS(5,2)|ABSORBING METHANEDIONE(5,1)|ACI COMMITTEE(5,1)|ACRE PLANTATION(5,1)|ADVANCED DECARBONIZATION(5,1)|HARDENED CONCRETE CARBONATION(5,1)|HORSE HAIRBRUSH(5,1)|KILN FUEL SULFUR CONTENT(5,1)|LIGHTWEIGHT AGGREGATE NATURE(5,1)|MANUFACTURED EXPANDED SHALE AGGREGATE(5,1)|NATURAL CRUSHED GRAVEL(5,1)|NONBIOLOGICAL CAPTURE(5,1)|OCEAN FERTILIZATION(5,1)|PAN PELLETIZER(5,1)|SLAG AGE(5,1)|STRIPPED CO2 COMPRESSION(5,1)|UNBURNED LIMESTONE(5,1)|DAY TESTING(4,4)|FLUE GAS COMPRESSION(4,4)|LIMESTONE CHEMICAL ANALYSIS(4,4)|QUICKLIME(4,4)|182 DAY AGE(4,3)|CA REACTION(4,3)|FOAM DENSITY(4,3)|GRANULE(4,3)|HARDENED FOAMED MATERIAL(4,3)|MG REACTION(4,3)|NA REACTION(4,3)|SIMULATED FLUE GAS(4,3)|CARBONATION DEPTH MEASUREMENT(4,2)|CEMENT MANUFACTURING FACILITY(4,2)|LIME MANUFACTURE(4,2)|METHANEDIONE GAS(4,2)|MOLTEN IRON(4,2)|UNCONFINED COMPRESSIVE STRENGTH(4,2)|AGRICULTURE GENETIC MANIPULATION(4,1)|ANNUAL CO2 SEQUESTRATION(4,1)|ANNUAL EMISSION(4,1)|BLAST FURNACE SLAG WT(4,1)|BLENDED PORTLAND CEMENT(4,1)|CARBONATE MINERAL(4,1)|CARBONATED CYLINDER(4,1)|CARBONATION CONTINUATION(4,1)|CARBONATION FULL DEPTH(4,1)|CARBONATION MEASUREMENT(4,1)|CARBONATION SITE(4,1)|CARBONATION ZONE(4,1)|CEMENT DECREASED MANUFACTURING(4,1)|CEMENT MIX(4,1)|CO2 ABSORPTION(4,1)|CO2 EMISSION(4,1)|CO2 FIXATION(4,1)|CO2 FOAM STABILITY(4,1)|COAL BED DEPTH(4,1)|COARSE AGGREGATE FRACTION(4,1)|COKE ASH(4,1)|COMPACTED FILL(4,1)|CRYOGENIC SEPARATION(4,1)|CURING ATMOSPHERE ABILITY(4,1)|DISPOSAL ISSUE(4,1)|DUST COLLECTING(4,1)|ECONOMIC BENEFIT(4,1)|EXHAUST STACK(4,1)|FOAM GENERATOR EXIT CONDUIT(4,1)|FOAM INSTABILITY BREAKDOWN(4,1)|FUTURE EXCAVATION(4,1)|GAL PAIL(4,1)|GEOLOGICAL MEDIA(4,1)|GLOBAL CONCERN(4,1)|INTAKE HOSE(4,1)|KILN EXHAUST(4,1)|KILN FURNACE(4,1)|LIBERATED CO2(4,1)|LIGHTWEIGHT AGGREGATE CONCRETE(4,1)|LIGHTWEIGHT CONCRETE AGGREGATE(4,1)|LIME KILN AGE(4,1)|MEASURED CARBONATION DEPTH(4,1)|METHANE REPLACEMENT(4,1)|METHANEDIONE(4,1)|METHANEDIONE CONTENT(4,1)|MIXTURE AGE SLAG(4,1)|MORTAR MIX(4,1)|PHENOLPHTHALEIN INDICATOR SOLUTION(4,1)|PLANNING PACKAGING(4,1)|POLYOL CONDENSATE FOAMING AGENT(4,1)|PRECOMBUSTION SEPARATION(4,1)|PREFOAMING SOLUTION EXPANSION(4,1)|PULVERIZED COAL COMBUSTION(4,1)|RETARDING ADMIXTURE(4,1)|RILEM TEST(4,1)|RUBBER HOSE EXTENSION(4,1)|SAMPLE CARBONATION(4,1)|SLAG TOTAL ASSUMPTION(4,1)|TRADE NAME MEARICRETE(4,1)|WESTERN LIME MANUFACTURING FACILITY(4,1)|WET UNLOADER(4,1)|WINTER CLIMATE(4,1)|COLD WINTER(3,4)|GEOGRAPHIC LOCATION(3,4)|LB FT(3,4)|NOMINAL SIZE AGGREGATE(3,4)|SLG(3,4)|FOAM GENERATION(3,3)|ABSORPTION SPECIFIC FINENESS(3,2)|AIR AGGREGATE(3,2)|BIOMASS(3,2)|DISPOSAL COST(3,2)|EXPERIMENT(3,2)|FINAL MIXTURE PROPORTION(3,2)|GRADE STREAM HEAT(3,2)|MASS CO2(3,2)|METRIC TON(3,2)|SPLITTING(3,2)|TESTING INDICATOR(3,2)|ADVANCEMENT CATALYST(3,1)|AGGREGATE FALL(3,1)|AGGREGATE RELATIVE FINENESS INDICATION(3,1)|ALKALI COMPOUND(3,1)|AMMONIA MANUFACTURING(3,1)|AVERAGE NET CO2(3,1)|BAG HOUSE(3,1)|CAPACITY TILTING(3,1)|CARBON RICH FEEDSTOCK(3,1)|CARBONATED DEPTH MEASUREMENT(3,1)|CARBONATION SLOW START(3,1)|CEMENT PRODUCTION(3,1)|CO2 SEPARATION(3,1)|COAL COMBUSTION CHAMBER(3,1)|COHESION(3,1)|COMPRESSION TESTING(3,1)|CURED MASS(3,1)|CYLINDRICAL TEST SPECIMEN(3,1)|DENSITY CONSISTENCY(3,1)|DOLOMITIC LIMESTONE(3,1)|ENHANCE CO2(3,1)|ENVIRONMENTAL RESEARCH FACILITY(3,1)|FLUE GAS FOAM(3,1)|FLUE GAS GLOBULE(3,1)|FOAM NOZZLE(3,1)|FOSSIL FUEL BURNING PLANT(3,1)|FROTH CONCENTRATE SOLUTION(3,1)|FURNACE LOCATION(3,1)|GENERATION PLANT(3,1)|GEOTECHNICAL PRODUCT(3,1)|GRADATION(3,1)|H2O CALCIUM HYDROXIDE(3,1)|INORGANIC MATRIX(3,1)|INORGANIC OXIDE ANALYSIS(3,1)|LB CU FT(3,1)|LOOSE PARTICLE(3,1)|METHANEDIONE SOURCE(3,1)|MINERAL DUST(3,1)|NONPHOTOSYNTHETIC(3,1)|OIL DEPLETION(3,1)|OXY FUEL COMBUSTION(3,1)|PERMEABILITY DIFFERENCE(3,1)|PLASTIC CYLINDER MOLD(3,1)|REDUCING METHANEDIONE PRODUCTION(3,1)|REMAINDER NITROGEN(3,1)|RUNNING MIXER(3,1)|SCRUBBER(3,1)|SLAG MANUFACTURING FACILITY(3,1)|SODIUM HYDROXIDE ABSORBENT(3,1)|STRENGTH GAIN(3,1)|TARGETED DRY DENSITY(3,1)|TERRESTRIAL ECOSYSTEM(3,1)|VACUUM SEALED BAG(3,1)|WRAPPED SAMPLE(3,1)|ZERO RATING(3,1)|GRAVITY(2,10)|2K2O(2,3)|2NA2O(2,3)|3H2O(2,3)|4H2O(2,3)|56 DAY AGE(2,3)|ASTM RESULT(2,3)|CALCIUM COMPOUND REACTION(2,3)|CAO MOLAR WEIGHT(2,3)|CARBONATE MATERIAL(2,3)|K2CO(2,3)|MAGNESIUM COMPOUND REACTION(2,3)|MOL SODIUM HYDROXIDE(2,3)|MOLAR WEIGHT MGO(2,3)|POTASSIUM COMPOUND REACTION(2,3)|SAMPLING(2,3)|SODIUM COMPOUND REACTION(2,3)|ZERO DAY AGE(2,3)|FINAL CURED PRODUCT(2,2)|FOSSIL FUEL COMBUSTION(2,2)|ABSORPTION TUBE(2,1)|ACETOGENESIS(2,1)|ADVANCED CHEMICAL(2,1)|AERATED CONCRETE PRODUCT(2,1)|AIR SLAG(2,1)|ALUMINO SILICATE(2,1)|ASPHALT(2,1)|AVAILABLE CAO CONTENT(2,1)|AVERAGE CO2(2,1)|BACKFILL(2,1)|BIOLOGICAL SEQUESTRATION(2,1)|BLAST FURNACE EXHAUST GAS(2,1)|BLENDER(2,1)|BRIQUETTER(2,1)|CARBON DIOXIDE(2,1)|CELLULAR CONCRETE STRUCTURE(2,1)|CEMENTITIOUS MATERIAL HYDRATION(2,1)|CHEESECLOTH(2,1)|CO2 PERCENT(2,1)|CO2 PRODUCTION(2,1)|CO2 REMOVAL(2,1)|CO2 SOURCE(2,1)|COARSENESS(2,1)|COMPACTION(2,1)|CONCRETE CONSTRUCTION YEAR(2,1)|CRUSHED AGGREGATE MATERIAL(2,1)|CURING CHAMBER AIR(2,1)|DATA REVIEW(2,1)|DIFFICULT PATHWAY(2,1)|DRY BASIS INITIAL(2,1)|ELASTIC FILM(2,1)|ELEMENTAL MERCURY(2,1)|EXPANDING COMPRESSED CO2 GAS(2,1)||(US20080245274)|CONTROLLED LOW STRENGTH MATERIAL(100,93)|METHANEDIONE(100,55)|PSI(100,49)|COMPRESSIVE STRENGTH(100,30)|GAS(100,25)|EXHAUST GAS(100,16)|COMBUSTION CHAMBER(100,9)|METHANEDIONE SEQUESTRATION(100,1)|LIME KIN DUST(39,1)|CEMENT KILN DUST(38,128)|FOAM(35,51)|LIME KILN DUST(34,125)|SLAG CEMENT(34,29)|CEMENTITIOUS MATERIAL(33,22)|CUBIC YARD(28,15)|FOAMING AGENT EXPANSION(28,3)|PORTLAND CEMENT PRODUCTION(24,1)|LIME PRODUCTION(22,1)|ANNUAL SEQUESTRATION ESTIMATE ASSUMPTION(19,3)|EXHAUST GAS COMPRESSION(19,3)|FOAMING AGENT(18,17)|HYDRATION PRODUCT(18,5)|INDUSTRIAL PRODUCTION PLANT(13,2)|PELLETIZING(13,1)|CUBIC FOOT(12,6)|METHANEDIONE PERMANENT SEQUESTRATION(12,2)|POWER COMBUSTION CHAMBER(12,1)|MOL CO2(11,12)|METHANEDIONE OCEAN SEQUESTRATION(11,1)|MOLTEN SLAG(10,5)|FOSSIL FUEL(9,6)|MOL NA2O(9,6)|MONTH AGE(9,5)|METHANEDIONE EMISSION(9,3)|SHAPING(9,2)|CARBONATION REACTION(8,4)|CARBONATION TESTING(8,3)|GRAVIMETRIC TESTING(8,3)|METHANEDIONE FOAM(8,2)|MULTICOMPONENT GAS STREAM(8,2)|AMERICAN CONCRETE INSTITUTE COMMITTEE(8,1)|LIME BLAST KILN(8,1)|PUMICE LIGHTWEIGHT AGGREGATE(8,1)|STEEL PRODUCTION(8,1)|WEIGHT PERCENT(8,1)|AL2O3(7,23)|MOL CALCIUM HYDROXIDE(7,9)|CO2 LB(7,6)|MOL K2O(7,6)|MOL KOH(7,6)|CO2 TON(7,3)|MOL MAGNESIA(7,3)|RAW INGREDIENT(7,3)|SEVEN DAY AGE(7,3)|CO2 PERMANENT SEQUESTRATION(7,1)|CRUSHED GRAVEL AGGREGATE(7,1)|DOLOMITIC LIME KILN DUST(7,1)|FOAMED MORTAR BATCH(7,1)|AMERICAN SOCIETY(6,2)|ELASTIZELL CORPORATION(6,2)|MINERAL AGGREGATE(6,2)|OUTDOOR STORAGE PILE(6,2)|PHENOLPHTHALEIN INDICATOR TEST(6,2)|SUMMER SEASON(6,2)|BOREAL WETLAND(6,1)|CEMENT KILN DUST TON(6,1)|CONCRETE NATURAL CARBONATION(6,1)|DEEP SALINE AQUIFER(6,1)|GRAVITY MODULUS STAINING(6,1)|PARTICLE SIZE FRACTION(6,1)|UNDERSIZE FINE AGGREGATE FRACTION(6,1)|WESTERN LIME CORPORATION(6,1)|FLY ASH(5,10)|MOL MG(5,6)|PERCENT CO2(5,4)|CURED CYLINDER(5,3)|CURING STATION(5,3)|EARLY AGE(5,3)|CARBONATION DIFFERENCE(5,2)|FIVE GALLON PAIL(5,2)|LATE AGE(5,2)|THERMOGRAVIMETRIC ANALYSIS(5,2)|ABSORBING METHANEDIONE(5,1)|ACI COMMITTEE(5,1)|ACRE PLANTATION(5,1)|ADVANCED DECARBONIZATION(5,1)|HARDENED CONCRETE CARBONATION(5,1)|HORSE HAIRBRUSH(5,1)|KILN FUEL SULFUR CONTENT(5,1)|LIGHTWEIGHT AGGREGATE NATURE(5,1)|MANUFACTURED EXPANDED SHALE AGGREGATE(5,1)|NATURAL CRUSHED GRAVEL(5,1)|NONBIOLOGICAL CAPTURE(5,1)|OCEAN FERTILIZATION(5,1)|PAN PELLETIZER(5,1)|SLAG AGE(5,1)|STRIPPED CO2 COMPRESSION(5,1)|UNBURNED LIMESTONE(5,1)|DAY TESTING(4,4)|FLUE GAS COMPRESSION(4,4)|LIMESTONE CHEMICAL ANALYSIS(4,4)|QUICKLIME(4,4)|182 DAY AGE(4,3)|CA REACTION(4,3)|FOAM DENSITY(4,3)|GRANULE(4,3)|HARDENED FOAMED MATERIAL(4,3)|MG REACTION(4,3)|NA REACTION(4,3)|SIMULATED FLUE GAS(4,3)|CARBONATION DEPTH MEASUREMENT(4,2)|CEMENT MANUFACTURING FACILITY(4,2)|LIME MANUFACTURE(4,2)|METHANEDIONE GAS(4,2)|MOLTEN IRON(4,2)|UNCONFINED COMPRESSIVE STRENGTH(4,2)|AGRICULTURE GENETIC MANIPULATION(4,1)|ANNUAL CO2 SEQUESTRATION(4,1)|ANNUAL EMISSION(4,1)|BLAST FURNACE SLAG WT(4,1)|BLENDED PORTLAND CEMENT(4,1)|CARBONATE MINERAL(4,1)|CARBONATED CYLINDER(4,1)|CARBONATION CONTINUATION(4,1)|CARBONATION FULL DEPTH(4,1)|CARBONATION MEASUREMENT(4,1)|CARBONATION SITE(4,1)|CARBONATION ZONE(4,1)|CEMENT DECREASED MANUFACTURING(4,1)|CEMENT MIX(4,1)|CO2 ABSORPTION(4,1)|CO2 EMISSION(4,1)|CO2 FIXATION(4,1)|CO2 FOAM STABILITY(4,1)|COAL BED DEPTH(4,1)|COARSE AGGREGATE FRACTION(4,1)|COKE ASH(4,1)|COMPACTED FILL(4,1)|CRYOGENIC SEPARATION(4,1)|CURING ATMOSPHERE ABILITY(4,1)|DISPOSAL ISSUE(4,1)|DUST COLLECTING(4,1)|ECONOMIC BENEFIT(4,1)|EXHAUST STACK(4,1)|FOAM GENERATOR EXIT CONDUIT(4,1)|FOAM INSTABILITY BREAKDOWN(4,1)|FUTURE EXCAVATION(4,1)|GAL PAIL(4,1)|GEOLOGICAL MEDIA(4,1)|GLOBAL CONCERN(4,1)|INTAKE HOSE(4,1)|KILN EXHAUST(4,1)|KILN FURNACE(4,1)|LIBERATED CO2(4,1)|LIGHTWEIGHT AGGREGATE CONCRETE(4,1)|LIGHTWEIGHT CONCRETE AGGREGATE(4,1)|LIME KILN AGE(4,1)|MEASURED CARBONATION DEPTH(4,1)|METHANE REPLACEMENT(4,1)|METHANEDIONE(4,1)|METHANEDIONE CONTENT(4,1)|MIXTURE AGE SLAG(4,1)|MORTAR MIX(4,1)|PHENOLPHTHALEIN INDICATOR SOLUTION(4,1)|PLANNING PACKAGING(4,1)|POLYOL CONDENSATE FOAMING AGENT(4,1)|PRECOMBUSTION SEPARATION(4,1)|PREFOAMING SOLUTION EXPANSION(4,1)|PULVERIZED COAL COMBUSTION(4,1)|RETARDING ADMIXTURE(4,1)|RILEM TEST(4,1)|RUBBER HOSE EXTENSION(4,1)|SAMPLE CARBONATION(4,1)|SLAG TOTAL ASSUMPTION(4,1)|TRADE NAME MEARICRETE(4,1)|WESTERN LIME MANUFACTURING FACILITY(4,1)|WET UNLOADER(4,1)|WINTER CLIMATE(4,1)|COLD WINTER(3,4)|GEOGRAPHIC LOCATION(3,4)|LB FT(3,4)|NOMINAL SIZE AGGREGATE(3,4)|SLG(3,4)|FOAM GENERATION(3,3)|ABSORPTION SPECIFIC FINENESS(3,2)|AIR AGGREGATE(3,2)|BIOMASS(3,2)|COMPRESSOR(3,2)|DISPOSAL COST(3,2)|EXPERIMENT(3,2)|FINAL MIXTURE PROPORTION(3,2)|GRADE STREAM HEAT(3,2)|MASS CO2(3,2)|METRIC TON(3,2)|SPLITTING(3,2)|TESTING INDICATOR(3,2)|ADVANCEMENT CATALYST(3,1)|AGGREGATE FALL(3,1)|AGGREGATE RELATIVE FINENESS INDICATION(3,1)|ALKALI COMPOUND(3,1)|AMMONIA MANUFACTURING(3,1)|AVERAGE NET CO2(3,1)|BAG HOUSE(3,1)|CAPACITY TILTING(3,1)|CARBON RICH FEEDSTOCK(3,1)|CARBONATED DEPTH MEASUREMENT(3,1)|CARBONATION SLOW START(3,1)|CEMENT PRODUCTION(3,1)|CO2 SEPARATION(3,1)|COAL COMBUSTION CHAMBER(3,1)|COHESION(3,1)|COMPRESSION TESTING(3,1)|CURED MASS(3,1)|CYLINDRICAL TEST SPECIMEN(3,1)|DENSITY CONSISTENCY(3,1)|DOLOMITIC LIMESTONE(3,1)|ENHANCE CO2(3,1)|ENVIRONMENTAL RESEARCH FACILITY(3,1)|FLUE GAS FOAM(3,1)|FLUE GAS GLOBULE(3,1)|FOAM NOZZLE(3,1)|FOSSIL FUEL BURNING PLANT(3,1)|FROTH CONCENTRATE SOLUTION(3,1)|FURNACE LOCATION(3,1)|GENERATION PLANT(3,1)|GEOTECHNICAL PRODUCT(3,1)|GRADATION(3,1)|INORGANIC MATRIX(3,1)|INORGANIC OXIDE ANALYSIS(3,1)|LB CU FT(3,1)|LOOSE PARTICLE(3,1)|METHANEDIONE SOURCE(3,1)|MINERAL DUST(3,1)|NONPHOTOSYNTHETIC(3,1)|OIL DEPLETION(3,1)|OXY FUEL COMBUSTION(3,1)|PERMEABILITY DIFFERENCE(3,1)|PLASTIC CYLINDER MOLD(3,1)|REDUCING METHANEDIONE PRODUCTION(3,1)|REMAINDER NITROGEN(3,1)|RUNNING MIXER(3,1)|SCRUBBER(3,1)|SLAG MANUFACTURING FACILITY(3,1)|SODIUM HYDROXIDE ABSORBENT(3,1)|STRENGTH GAIN(3,1)|TARGETED DRY DENSITY(3,1)|TERRESTRIAL ECOSYSTEM(3,1)|VACUUM SEALED BAG(3,1)|WRAPPED SAMPLE(3,1)|ZERO RATING(3,1)|GRAVITY(2,10)|2K2O(2,3)|2NA2O(2,3)|3H2O(2,3)|4H2O(2,3)|56 DAY AGE(2,3)|ASTM RESULT(2,3)|CALCIUM COMPOUND REACTION(2,3)|CAO MOLAR WEIGHT(2,3)|CARBONATE MATERIAL(2,3)|K2CO(2,3)|MAGNESIUM COMPOUND REACTION(2,3)|MOL SODIUM HYDROXIDE(2,3)|MOLAR WEIGHT MGO(2,3)|POTASSIUM COMPOUND REACTION(2,3)|SAMPLING(2,3)|SODIUM COMPOUND REACTION(2,3)|ZERO DAY AGE(2,3)|FINAL CURED PRODUCT(2,2)|FOSSIL FUEL COMBUSTION(2,2)|ABSORPTION TUBE(2,1)|ACETOGENESIS(2,1)|ADVANCED CHEMICAL(2,1)|AERATED CONCRETE PRODUCT(2,1)|AIR SLAG(2,1)|ALUMINO SILICATE(2,1)|ASPHALT(2,1)|AVAILABLE CAO CONTENT(2,1)|AVERAGE CO2(2,1)|BACKFILL(2,1)|BIOLOGICAL SEQUESTRATION(2,1)|BLAST FURNACE EXHAUST GAS(2,1)|BLENDER(2,1)|BRIQUETTER(2,1)|CARBON DIOXIDE(2,1)|CELLULAR CONCRETE STRUCTURE(2,1)|CEMENTITIOUS MATERIAL HYDRATION(2,1)|CHEESECLOTH(2,1)|CO2 PERCENT(2,1)|CO2 PRODUCTION(2,1)|CO2 REMOVAL(2,1)|CO2 SOURCE(2,1)|COARSENESS(2,1)|COMPACTION(2,1)|CONCRETE CONSTRUCTION YEAR(2,1)|CRUSHED AGGREGATE MATERIAL(2,1)|CURING CHAMBER AIR(2,1)|DATA REVIEW(2,1)|DIFFICULT PATHWAY(2,1)|DRY BASIS INITIAL(2,1)|ELASTIC FILM(2,1)|ELEMENTAL MERCURY(2,1)|EXPANDING COMPRESSED CO2 GAS(2,1)||(US7390444)|CONTROLLED LOW STRENGTH MATERIAL(100,164)|METHANEDIONE(100,72)|FLUE GAS(100,70)|COMPRESSIVE STRENGTH(100,36)|PSI(100,28)|GAS(100,19)|COMBUSTION CHAMBER(100,9)|METHANEDIONE SEQUESTRATION(100,1)|FOAM(34,66)|FLY ASH(30,118)|FOAMING AGENT EXPANSION(28,3)|COAL BURNING(25,3)|VIEWPOINT(23,1)|CEMENTITIOUS MATERIAL(22,11)|CUBIC YARD(19,13)|FOAMING AGENT(19,13)|HYDRATION PRODUCT(18,5)|BURNING POWER PLANT(17,3)|FLUE GAS COMPRESSION(14,5)|NATURALLY OCCURRING MINERAL(14,2)|PELLETIZING(13,1)|METHANEDIONE PERMANENT SEQUESTRATION(12,2)|METHANEDIONE EMISSION(11,4)|METHANEDIONE OCEAN SEQUESTRATION(11,1)|SIMULATED FLUE GAS(10,17)|OAK CREEK FLY ASH(10,2)|SHAPING(9,2)|PUMICE(8,6)|CARBONATION REACTION(8,4)|CLAY LUMP(8,4)|MULTICOMPONENT GAS STREAM(8,2)|AMERICAN CONCRETE INSTITUTE COMMITTEE(8,1)|METHANEDIONE STARTED CARBONATION(8,1)|WEIGHT PERCENT(8,1)|FLY ASH WT(7,5)|AMERICAN SOCIETY(7,3)|LATE AGE(7,3)|CO2 PERMANENT SEQUESTRATION(7,1)|SEQUESTERING METHANEDIONE(7,1)|LB YD(6,18)|CUBIC FOOT(6,5)|MOL CO2(6,4)|TRIAL MIXTURE PROPORTION(6,4)|CARBONATION MEASUREMENT(6,2)|CONCRETE AGGREGATE(6,2)|ELASTIZELL CORPORATION(6,2)|OUTDOOR STORAGE PILE(6,2)|SUMMER SEASON(6,2)|BOREAL WETLAND(6,1)|CONCRETE NATURAL CARBONATION(6,1)|DEEP SALINE AQUIFER(6,1)|PARTICLE SIZE FRACTION(6,1)|UNDERSIZE FINE AGGREGATE FRACTION(6,1)|WASTE HEAT(6,1)|LB FT(5,13)|AL2O3(5,10)|DRY WT(5,6)|FOAM GENERATION(5,4)|CURING STATION(5,3)|SIEVE PERCENT(5,3)|MINERAL ADMIXTURE(5,2)|MOL NA2O(5,2)|PARAMETER ASTM(5,2)|ABSORBING METHANEDIONE(5,1)|ACI COMMITTEE(5,1)|ACRE PLANTATION(5,1)|ADVANCED DECARBONIZATION(5,1)|ASR MINIMIZATION(5,1)|FINE AGGREGATE ASTM(5,1)|FINE AGGREGATE GRADATION(5,1)|HARDENED CONCRETE CARBONATION(5,1)|HORSE HAIRBRUSH(5,1)|LIGHTWEIGHT AGGREGATE NATURE(5,1)|LIME CAO(5,1)|NONBIOLOGICAL CAPTURE(5,1)|OCEAN FERTILIZATION(5,1)|PAN PELLETIZER(5,1)|STRIPPED CO2 COMPRESSION(5,1)|SUBBITUMINOUS COAL(5,1)|COMPRESSED GAS(4,4)|DAY TESTING(4,4)|FLY ASH STORAGE SILO(4,4)|PORTLAND CEMENT(4,4)|EXPERIMENT(4,3)|MOL CALCIUM HYDROXIDE(4,3)|SPLITTING(4,3)|ASTM CLASS C(4,2)|FOSSIL FUEL BURNING PLANT(4,2)|HARDENED DENSITY(4,2)|MOL K2O(4,2)|MOL KOH(4,2)|UNCONFINED COMPRESSIVE STRENGTH(4,2)|AGRICULTURE GENETIC MANIPULATION(4,1)|ANNUAL EMISSION(4,1)|AUTOCLAVE EXPANSION(4,1)|BAG HOUSE(4,1)|CARBONATION COMPARISON(4,1)|CARBONATION INDICATION(4,1)|CARBONATION TESTING(4,1)|CEMENT DECREASED MANUFACTURING(4,1)|CO2 ABSORPTION(4,1)|CO2 EMISSION(4,1)|CO2 FIXATION(4,1)|COAL BED DEPTH(4,1)|COARSE AGGREGATE ASTM(4,1)|COARSE AGGREGATE FRACTION(4,1)|COARSE AGGREGATE GRADATION(4,1)|COMBUSTION FLY ASH(4,1)|COMPACTED FILL(4,1)|CONCRETE PARTICLE(4,1)|CRYOGENIC SEPARATION(4,1)|EXHAUST STACK(4,1)|FOAM APPEARANCE(4,1)|FOAM GENERATOR EXIT CONDUIT(4,1)|FOAM TEST SPECIMEN(4,1)|FUTURE EXCAVATION(4,1)|GEOLOGICAL MEDIA(4,1)|GLASSY SPHERE(4,1)|INTAKE HOSE(4,1)|LOCATION FRIABLE CLASS(4,1)|METHANE REPLACEMENT(4,1)|METHANEDIONE(4,1)|MOL MAGNESIA(4,1)|MORTAR MIX(4,1)|NITROGEN NOX REDUCTION TREATMENT(4,1)|PHENOLPHTHALEIN INDICATOR SOLUTION(4,1)|POLYOL CONDENSATE FOAMING AGENT(4,1)|PRECOMBUSTION SEPARATION(4,1)|PREFOAMING SOLUTION EXPANSION(4,1)|PULVERIZED COAL COMBUSTION(4,1)|RILEM TEST(4,1)|RUBBER HOSE EXTENSION(4,1)|SAMPLE CARBONATION(4,1)|TEST CYLINDER INSUFFICIENT CONSOLIDATION(4,1)|TRADE NAME MEARLCRETE(4,1)|WET UNLOADER(4,1)|COLD WINTER(3,4)|GEOGRAPHIC LOCATION(3,4)|BIOMASS(3,2)|COMPRESSOR(3,2)|CURING ROOM(3,2)|DIOXOTITANIUM(3,2)|DISPOSAL(3,2)|GRADE STREAM HEAT(3,2)|METRIC TON(3,2)|MOL MG(3,2)|SOUNDNESS(3,2)|ADVANCEMENT CATALYST(3,1)|AMMONIA MANUFACTURING(3,1)|CARBON RICH FEEDSTOCK(3,1)|CEMENT MANUFACTURING(3,1)|CO2 SEPARATION(3,1)|COAL COMBUSTION CHAMBER(3,1)|COARSE STANDARD(3,1)|COHESION(3,1)|CURED MASS(3,1)|CYLINDRICAL TEST SPECIMEN(3,1)|ENHANCE CO2(3,1)|ENVIRONMENTAL RESEARCH FACILITY(3,1)|FINE BUBBLE(3,1)|FLUE GAS GLOBULE(3,1)|FLY ASH TOTAL ASSUMPTION(3,1)|FOAM NOZZLE(3,1)|FROTH CONCENTRATE SOLUTION(3,1)|FURNACE LOCATION(3,1)|GENERATOR FITTING(3,1)|H2O CALCIUM HYDROXIDE(3,1)|INORGANIC MATRIX(3,1)|INORGANIC PARTICLE(3,1)|LOOSE PARTICLE(3,1)|MAINTENANCE GATE(3,1)|METHANEDIONE GAS(3,1)|METHANEDIONE SOURCE(3,1)|NONPHOTOSYNTHETIC(3,1)|OIL DEPLETION(3,1)|OXY FUEL COMBUSTION(3,1)|REDUCING METHANEDIONE PRODUCTION(3,1)|REMAINDER NITROGEN(3,1)|RUNNING MIXER(3,1)|TERRESTRIAL ECOSYSTEM(3,1)|UNBURNED CARBON(3,1)|FINAL CURED PRODUCT(2,2)|ACETOGENESIS(2,1)|ADVANCED CHEMICAL(2,1)|AERATED CONCRETE PRODUCT(2,1)|BACKFILL(2,1)|BASIC MIXTURE(2,1)|BIOLOGICAL SEQUESTRATION(2,1)|BLENDER(2,1)|BRIQUETTER(2,1)|CA REACTION(2,1)|CARBON DIOXIDE(2,1)|CARBON PARTICLE(2,1)|CELLULAR CONCRETE STRUCTURE(2,1)|CEMENTITIOUS MATERIAL HYDRATION(2,1)|CLASS ANALYSIS PARAMETER(2,1)|CO2 PRODUCTION(2,1)|CO2 REMOVAL(2,1)|CO2 SEQUESTRATION(2,1)|CO2 SOURCE(2,1)|COMPACTION(2,1)|COMPRESSED AIR CARBONATION(2,1)|CONCRETE CONSTRUCTION YEAR(2,1)|DESIGNATION CONSTRUCTION STANDARD(2,1)|ELASTIC FILM(2,1)|ELECTROSTATIC PRECIPITATOR(2,1)|ELEMENTAL MERCURY(2,1)|FEASIBILITY(2,1)|FERMENTATION(2,1)|FINAL MIXTURE PROPORTION(2,1)|FLOOR SLAB INTERIOR(2,1)||(US20060185560)|CONTROLLED LOW STRENGTH MATERIAL(100,161)|METHANEDIONE(100,68)|FLUE GAS(100,66)|COMPRESSIVE STRENGTH(100,36)|PSI(100,28)|GAS(100,18)|COMBUSTION CHAMBER(100,9)|METHANEDIONE SEQUESTRATION(100,1)|FOAM(27,60)|FLY ASH(26,114)|CEMENTITIOUS MATERIAL(22,11)|COAL BURNING(21,1)|CUBIC YARD(19,13)|FOAMING AGENT(19,13)|HYDRATION PRODUCT(18,5)|NATURALLY OCCURRING MINERAL(14,2)|BURNING POWER PLANT(14,1)|PELLETIZING(13,1)|METHANEDIONE PERMANENT SEQUESTRATION(12,2)|METHANEDIONE OCEAN SEQUESTRATION(11,1)|SIMULATED FLUE GAS(10,17)|OAK CREEK FLY ASH(10,2)|METHANEDIONE EMISSION(9,3)|SHAPING(9,2)|PUMICE(8,6)|CARBONATION REACTION(8,4)|CLAY LUMP(8,4)|MULTICOMPONENT GAS STREAM(8,2)|AMERICAN CONCRETE INSTITUTE COMMITTEE(8,1)|METHANEDIONE STARTED CARBONATION(8,1)|WEIGHT PERCENT(8,1)|FLY ASH WT(7,5)|AMERICAN SOCIETY(7,3)|LATE AGE(7,3)|CO2 PERMANENT SEQUESTRATION(7,1)|SEQUESTERING METHANEDIONE(7,1)|LB YD(6,18)|CUBIC FOOT(6,5)|MOL CO2(6,4)|TRIAL MIXTURE PROPORTION(6,4)|CARBONATION MEASUREMENT(6,2)|CONCRETE AGGREGATE(6,2)|ELASTIZELL CORPORATION(6,2)|OUTDOOR STORAGE PILE(6,2)|SUMMER SEASON(6,2)|BOREAL WETLAND(6,1)|CONCRETE NATURAL CARBONATION(6,1)|DEEP SALINE AQUIFER(6,1)|PARTICLE SIZE FRACTION(6,1)|UNDERSIZE FINE AGGREGATE FRACTION(6,1)|WASTE HEAT(6,1)|LB FT(5,13)|AL2O3(5,10)|DRY WT(5,6)|FOAM GENERATION(5,4)|CURING STATION(5,3)|SIEVE PERCENT(5,3)|MINERAL ADMIXTURE(5,2)|MOL NA2O(5,2)|PARAMETER ASTM(5,2)|ABSORBING METHANEDIONE(5,1)|ACI COMMITTEE(5,1)|ACRE PLANTATION(5,1)|ADVANCED DECARBONIZATION(5,1)|ASR MINIMIZATION(5,1)|FINE AGGREGATE ASTM(5,1)|FINE AGGREGATE GRADATION(5,1)|HARDENED CONCRETE CARBONATION(5,1)|HORSE HAIRBRUSH(5,1)|LIGHTWEIGHT AGGREGATE NATURE(5,1)|LIME CAO(5,1)|NONBIOLOGICAL CAPTURE(5,1)|OCEAN FERTILIZATION(5,1)|PAN PELLETIZER(5,1)|STRIPPED CO2 COMPRESSION(5,1)|SUBBITUMINOUS COAL(5,1)|DAY TESTING(4,4)|FLY ASH STORAGE SILO(4,4)|PORTLAND CEMENT(4,4)|EXPERIMENT(4,3)|FLUE GAS COMPRESSION(4,3)|MOL CALCIUM HYDROXIDE(4,3)|SPLITTING(4,3)|ASTM CLASS C(4,2)|HARDENED DENSITY(4,2)|MOL K2O(4,2)|MOL KOH(4,2)|UNCONFINED COMPRESSIVE STRENGTH(4,2)|AGRICULTURE GENETIC MANIPULATION(4,1)|ANNUAL EMISSION(4,1)|AUTOCLAVE EXPANSION(4,1)|BAG HOUSE(4,1)|CARBONATION COMPARISON(4,1)|CARBONATION INDICATION(4,1)|CARBONATION TESTING(4,1)|CEMENT DECREASED MANUFACTURING(4,1)|CO2 ABSORPTION(4,1)|CO2 EMISSION(4,1)|CO2 FIXATION(4,1)|COAL BED DEPTH(4,1)|COARSE AGGREGATE ASTM(4,1)|COARSE AGGREGATE FRACTION(4,1)|COARSE AGGREGATE GRADATION(4,1)|COMBUSTION FLY ASH(4,1)|COMPACTED FILL(4,1)|CONCRETE PARTICLE(4,1)|CRYOGENIC SEPARATION(4,1)|EXHAUST STACK(4,1)|FOAM APPEARANCE(4,1)|FOAM GENERATOR EXIT CONDUIT(4,1)|FOAM TEST SPECIMEN(4,1)|FUTURE EXCAVATION(4,1)|GEOLOGICAL MEDIA(4,1)|GLASSY SPHERE(4,1)|INTAKE HOSE(4,1)|LOCATION FRIABLE CLASS(4,1)|METHANE REPLACEMENT(4,1)|METHANEDIONE(4,1)|MOL MAGNESIA(4,1)|MORTAR MIX(4,1)|NITROGEN NOX REDUCTION TREATMENT(4,1)|PHENOLPHTHALEIN INDICATOR SOLUTION(4,1)|POLYOL CONDENSATE FOAMING AGENT(4,1)|PRECOMBUSTION SEPARATION(4,1)|PREFOAMING SOLUTION EXPANSION(4,1)|PULVERIZED COAL COMBUSTION(4,1)|RILEM TEST(4,1)|RUBBER HOSE EXTENSION(4,1)|SAMPLE CARBONATION(4,1)|TEST CYLINDER INSUFFICIENT CONSOLIDATION(4,1)|TRADE NAME MEARLCRETE(4,1)|WET UNLOADER(4,1)|COLD WINTER(3,4)|GEOGRAPHIC LOCATION(3,4)|BIOMASS(3,2)|COMPRESSOR(3,2)|CURING ROOM(3,2)|DIOXOTITANIUM(3,2)|DISPOSAL(3,2)|GRADE STREAM HEAT(3,2)|METRIC TON(3,2)|MOL MG(3,2)|SOUNDNESS(3,2)|ADVANCEMENT CATALYST(3,1)|AMMONIA MANUFACTURING(3,1)|CARBON RICH FEEDSTOCK(3,1)|CEMENT MANUFACTURING(3,1)|CO2 SEPARATION(3,1)|COAL COMBUSTION CHAMBER(3,1)|COARSE STANDARD(3,1)|COHESION(3,1)|CURED MASS(3,1)|CYLINDRICAL TEST SPECIMEN(3,1)|ENHANCE CO2(3,1)|ENVIRONMENTAL RESEARCH FACILITY(3,1)|FINE BUBBLE(3,1)|FLUE GAS GLOBULE(3,1)|FOAM NOZZLE(3,1)|FOSSIL FUEL BURNING PLANT(3,1)|FROTH CONCENTRATE SOLUTION(3,1)|FURNACE LOCATION(3,1)|GENERATOR FITTING(3,1)|H2O CALCIUM HYDROXIDE(3,1)|INORGANIC MATRIX(3,1)|INORGANIC PARTICLE(3,1)|LOOSE PARTICLE(3,1)|MAINTENANCE GATE(3,1)|METHANEDIONE GAS(3,1)|METHANEDIONE SOURCE(3,1)|NONPHOTOSYNTHETIC(3,1)|OIL DEPLETION(3,1)|OXY FUEL COMBUSTION(3,1)|REDUCING METHANEDIONE PRODUCTION(3,1)|REMAINDER NITROGEN(3,1)|RUNNING MIXER(3,1)|TERRESTRIAL ECOSYSTEM(3,1)|UNBURNED CARBON(3,1)|FINAL CURED PRODUCT(2,2)|ACETOGENESIS(2,1)|ADVANCED CHEMICAL(2,1)|AERATED CONCRETE PRODUCT(2,1)|BACKFILL(2,1)|BASIC MIXTURE(2,1)|BIOLOGICAL SEQUESTRATION(2,1)|BLENDER(2,1)|BRIQUETTER(2,1)|CA REACTION(2,1)|CARBON DIOXIDE(2,1)|CARBON PARTICLE(2,1)|CELLULAR CONCRETE STRUCTURE(2,1)|CEMENTITIOUS MATERIAL HYDRATION(2,1)|CLASS ANALYSIS PARAMETER(2,1)|CO2 PRODUCTION(2,1)|CO2 REMOVAL(2,1)|CO2 SEQUESTRATION(2,1)|CO2 SOURCE(2,1)|COMPACTION(2,1)|COMPRESSED AIR CARBONATION(2,1)|CONCRETE CONSTRUCTION YEAR(2,1)|DESIGNATION CONSTRUCTION STANDARD(2,1)|ELASTIC FILM(2,1)|ELECTROSTATIC PRECIPITATOR(2,1)|ELEMENTAL MERCURY(2,1)|FEASIBILITY(2,1)|FERMENTATION(2,1)|FINAL MIXTURE PROPORTION(2,1)|FLOOR SLAB INTERIOR(2,1)|FLUE GAS CONTEXT(2,1)||(CA2537383)|CONTROLLED LOW STRENGTH MATERIAL(100,171)|METHANEDIONE(100,67)|FLUE GAS(100,66)|COMPRESSIVE STRENGTH(100,37)|PSI(100,31)|GAS(100,18)|COMBUSTION CHAMBER(100,9)|METHANEDIONE SEQUESTRATION(100,2)|FOAM(37,52)|FLY ASH(33,114)|CEMENTITIOUS MATERIAL(29,11)|CUBIC YARD(25,13)|FOAMING AGENT(25,13)|HYDRATION PRODUCT(23,5)|OAK CREEK FLY ASH(19,4)|NATURALLY OCCURRING MINERAL(18,2)|PELLETIZING(18,1)|METHANEDIONE PERMANENT SEQUESTRATION(16,2)|METHANEDIONE OCEAN SEQUESTRATION(14,1)|SIMULATED FLUE GAS(13,17)|METHANEDIONE EMISSION(12,3)|AMERICAN CONCRETE INSTITUTE(12,2)|SHAPING(12,2)|CARBONATION DEPTH(11,4)|STRENGTH MATERIAL(11,3)|COARSE AAAREAATE GRADATION(11,1)|METHANEDIONE STARTED CARBONATION(11,1)|TRIAL MIXTURE PROPORTION(10,5)|CARBONATION REACTION(10,4)|CLAY LUMP(10,4)|MULTICOMPONENT GAS STREAM(10,2)|CONCRETE AGGREGATE SOUNDNESS(10,1)|WEIGHT PERCENT(10,1)|CUBIC FOOT(9,5)|FLY ASH WT(9,5)|LATE AGE(9,3)|ELASTIZELL CORPORATION(9,2)|OUTDOOR STORAGE PILE(9,2)|SUMMER SEASON(9,2)|CO2 PERMANENT SEQUESTRATION(9,1)|LB YD(8,17)|AMERICAN SOCIETY(8,2)|BOREAL WETLAND(8,1)|CONCRETE NATURAL CARBONATION(8,1)|CYO CARBONATION(8,1)|DEEP SALINE AQUIFER(8,1)|FINE AQCTREQATE GRADATION(8,1)|PARTICLE SIZE FRACTION(8,1)|UNDERSIZE FINE AGGREGATE FRACTION(8,1)|WASTE HEAT(8,1)|DRY WT(7,6)|CURING STATION(7,3)|MINERAL ADMIXTURE(7,2)|57962E 05 MOT CO2(7,1)|ABSORBING METHANEDIONE(7,1)|ACRE PLANTATION(7,1)|ADVANCED DECARBONIZATION(7,1)|ASR MINIMIZATION(7,1)|HARDENED CONCRETE CARBONATION MEASUREMENT(7,1)|HORSE HAIRBRUSH(7,1)|LIGHTWEIGHT AGGREGATE NATURE(7,1)|LIME CAO(7,1)|NONBIOLOGICAL CAPTURE(7,1)|OCEAN FERTILIZATION(7,1)|OK CARBONATION(7,1)|PAN PELLETIZER(7,1)|STRIPPED CO2 COMPRESSION(7,1)|SUBBITUMINOUS COAL(7,1)|DAY TESTING(6,4)|FLY ASH STORAGE SILO(6,4)|FOAM GENERATION(6,4)|PORTLAND CEMENT(6,4)|HARDENED DENSITY(6,2)|UNCONFINED COMPRESSIVE STRENGTH(6,2)|AGRICULTURE GENETIC MANIPULATION(6,1)|CARBONATION EVALUATION(6,1)|CARBONATION INDICATION(6,1)|CARBONATION TESTING(6,1)|COAL BED DEPTH(6,1)|FINE AGGREGATE ASTM(6,1)|FOAM GENERATOR EXIT CONDUIT(6,1)|FOAM TEST SPECIMEN(6,1)|FUTURE EXCAVATION(6,1)|GLASSY SPHERE(6,1)|POLYOL CONDENSATE FOAMING AGENT(6,1)|PULVERIZED COAL COMBUSTION(6,1)|TEST CYLINDER INSUFFICIENT CONSOLIDATION(6,1)|COMPRESSED AIR(5,22)|FLUE GAS COMPRESSION(5,3)|SIEVE OPENING(5,3)|SPLITTING(5,3)|ASTM CLASS C(5,2)|ANNUAL EMISSION(5,1)|AUTOCLAVE EXPANSION(5,1)|BAG HOUSE(5,1)|CARBONATION COMPARISON(5,1)|CEMENT DECREASED MANUFACTURING(5,1)|CLASS DESIGNATION(5,1)|CO2 ABSORPTION(5,1)|CO2 FIXATION(5,1)|COARSE AGGREGATE ASTM(5,1)|COARSE AGGREGATE FRACTION(5,1)|COMBUSTION FLY ASH(5,1)|COMPACTED FILL(5,1)|CONCRETE AGGREGATE LIMIT(5,1)|CRYOGENIC SEPARATION(5,1)|EXHAUST STACK(5,1)|EXPERIMENTAL OVERVIEW(5,1)|FINE BUBBLE(5,1)|FRIABLE PARTICLE STANDARD(5,1)|GEOLOGICAL MEDIA(5,1)|INTAKE HOSE(5,1)|METHANE REPLACEMENT(5,1)|METHANEDIONE(5,1)|MORTAR MIX(5,1)|NITROGEN NOX REDUCTION TREATMENT(5,1)|PHENOLPHTHALEIN INDICATOR SOLUTION(5,1)|PRECOMBUSTION SEPARATION(5,1)|PREFOAMING SOLUTION EXPANSION(5,1)|REGULATOR FITTING(5,1)|RILEM TEST(5,1)|RUBBER HOSE EXTENSION(5,1)|SAMPLE CARBONATION(5,1)|TRADE NAME MEARLCRETE(5,1)|WET UNLOADER(5,1)|COLD WINTER(4,4)|GEOGRAPHIC LOCATION(4,4)|RXN(4,4)|BIOMASS(4,2)|COMMENT(4,2)|COMMITTEE(4,2)|COMPRESSOR(4,2)|CURING ROOM(4,2)|DISPOSAL(4,2)|GRADE STREAM HEAT(4,2)|METRIC TON(4,2)|ADVANCEMENT CATALYST(4,1)|AMMONIA MANUFACTURING(4,1)|ANALYSIS PARAMETER(4,1)|CARBON RICH FEEDSTOCK(4,1)|CEMENT MANUFACTURING(4,1)|CO2 SEPARATION(4,1)|COAL COMBUSTION CHAMBER(4,1)|COHESION(4,1)|CURED MASS(4,1)|CYLINDRICAL TEST SPECIMEN(4,1)|ENHANCE CO2(4,1)|ENVIRONMENTAL RESEARCH FACILITY(4,1)|ESTIMATION CALCULATION(4,1)|FLUE GAS GLOBULE(4,1)|FOAM NOZZLE(4,1)|FOSSIL FUEL BURNING PLANT(4,1)|FROTH CONCENTRATE SOLUTION(4,1)|FURNACE LOCATION(4,1)|INORGANIC MATRIX(4,1)|INORGANIC PARTICLE(4,1)|LOOSE PARTICLE(4,1)|MAINTENANCE GATE(4,1)|METHANEDIONE GAS(4,1)|METHANEDIONE SOURCE(4,1)|NONPHOTOSYNTHETIC(4,1)|OIL DEPLETION(4,1)|OXY FUEL COMBUSTION(4,1)|PUMICE FINE(4,1)|REDUCING METHANEDIONE PRODUCTION(4,1)|REMAINDER NITROGEN(4,1)|RUNNING MIXER(4,1)|TANK FILLING(4,1)|TERRESTRIAL ECOSYSTEM(4,1)|UNBURNED CARBON(4,1)|MIXTURE NUMBER(3,11)|FOAM VOLUME(3,3)|MAGNESIA(3,3)|FINAL CURED PRODUCT(3,2)|ACETOGENESIS(3,1)|ADVANCED CHEMICAL(3,1)|AERATED CONCRETE PRODUCT(3,1)|BACKFILL(3,1)|BASIC MIXTURE(3,1)|BIOLOGICAL SEQUESTRATION(3,1)|BLENDER(3,1)|BRIQUETTER(3,1)|CA REACTION(3,1)|CARBON PARTICLE(3,1)|CELLULAR CONCRETE STRUCTURE(3,1)|CEMENTITIOUS MATERIAL HYDRATION(3,1)|CO2 PRODUCTION(3,1)|CO2 REMOVAL(3,1)|CO2 SEQUESTRATION(3,1)|COMPACTION(3,1)|CONCRETE CONSTRUCTION YEAR(3,1)|ELASTIC FILM(3,1)|ELECTROSTATIC PRECIPITATOR(3,1)|ELEMENTAL MERCURY(3,1)|FEASIBILITY(3,1)|FERMENTATION(3,1)|FINAL MIXTURE PROPORTION(3,1)|FLOOR SLAB INTERIOR(3,1)|FLUE GAS CONTEXT(3,1)|FOAM PRODUCTION(3,1)|FOOTING(3,1)|FOREST(3,1)|FOUNDATION(3,1)||(CA2537383)|CONTROLLED LOW STRENGTH MATERIAL(100,171)|METHANEDIONE(100,67)|FLUE GAS(100,66)|COMPRESSIVE STRENGTH(100,37)|PSI(100,31)|GAS(100,18)|COMBUSTION CHAMBER(100,9)|METHANEDIONE SEQUESTRATION(100,2)|FOAM(37,52)|FLY ASH(33,114)|CEMENTITIOUS MATERIAL(29,11)|CUBIC YARD(25,13)|FOAMING AGENT(25,13)|HYDRATION PRODUCT(23,5)|OAK CREEK FLY ASH(19,4)|NATURALLY OCCURRING MINERAL(18,2)|PELLETIZING(18,1)|METHANEDIONE PERMANENT SEQUESTRATION(16,2)|METHANEDIONE OCEAN SEQUESTRATION(14,1)|SIMULATED FLUE GAS(13,17)|METHANEDIONE EMISSION(12,3)|AMERICAN CONCRETE INSTITUTE(12,2)|SHAPING(12,2)|CARBONATION DEPTH(11,4)|STRENGTH MATERIAL(11,3)|COARSE AAAREAATE GRADATION(11,1)|METHANEDIONE STARTED CARBONATION(11,1)|TRIAL MIXTURE PROPORTION(10,5)|CARBONATION REACTION(10,4)|CLAY LUMP(10,4)|MULTICOMPONENT GAS STREAM(10,2)|CONCRETE AGGREGATE SOUNDNESS(10,1)|WEIGHT PERCENT(10,1)|CUBIC FOOT(9,5)|FLY ASH WT(9,5)|LATE AGE(9,3)|ELASTIZELL CORPORATION(9,2)|OUTDOOR STORAGE PILE(9,2)|SUMMER SEASON(9,2)|CO2 PERMANENT SEQUESTRATION(9,1)|LB YD(8,17)|AMERICAN SOCIETY(8,2)|BOREAL WETLAND(8,1)|CONCRETE NATURAL CARBONATION(8,1)|CYO CARBONATION(8,1)|DEEP SALINE AQUIFER(8,1)|FINE AQCTREQATE GRADATION(8,1)|PARTICLE SIZE FRACTION(8,1)|UNDERSIZE FINE AGGREGATE FRACTION(8,1)|WASTE HEAT(8,1)|DRY WT(7,6)|CURING STATION(7,3)|MINERAL ADMIXTURE(7,2)|57962E 05 MOT CO2(7,1)|ABSORBING METHANEDIONE(7,1)|ACRE PLANTATION(7,1)|ADVANCED DECARBONIZATION(7,1)|ASR MINIMIZATION(7,1)|HARDENED CONCRETE CARBONATION MEASUREMENT(7,1)|HORSE HAIRBRUSH(7,1)|LIGHTWEIGHT AGGREGATE NATURE(7,1)|LIME CAO(7,1)|NONBIOLOGICAL CAPTURE(7,1)|OCEAN FERTILIZATION(7,1)|OK CARBONATION(7,1)|PAN PELLETIZER(7,1)|STRIPPED CO2 COMPRESSION(7,1)|SUBBITUMINOUS COAL(7,1)|DAY TESTING(6,4)|FLY ASH STORAGE SILO(6,4)|FOAM GENERATION(6,4)|PORTLAND CEMENT(6,4)|HARDENED DENSITY(6,2)|UNCONFINED COMPRESSIVE STRENGTH(6,2)|AGRICULTURE GENETIC MANIPULATION(6,1)|CARBONATION EVALUATION(6,1)|CARBONATION INDICATION(6,1)|CARBONATION TESTING(6,1)|COAL BED DEPTH(6,1)|FINE AGGREGATE ASTM(6,1)|FOAM GENERATOR EXIT CONDUIT(6,1)|FOAM TEST SPECIMEN(6,1)|FUTURE EXCAVATION(6,1)|GLASSY SPHERE(6,1)|POLYOL CONDENSATE FOAMING AGENT(6,1)|PULVERIZED COAL COMBUSTION(6,1)|TEST CYLINDER INSUFFICIENT CONSOLIDATION(6,1)|COMPRESSED AIR(5,22)|FLUE GAS COMPRESSION(5,3)|SIEVE OPENING(5,3)|SPLITTING(5,3)|ASTM CLASS C(5,2)|ANNUAL EMISSION(5,1)|AUTOCLAVE EXPANSION(5,1)|BAG HOUSE(5,1)|CARBONATION COMPARISON(5,1)|CEMENT DECREASED MANUFACTURING(5,1)|CLASS DESIGNATION(5,1)|CO2 ABSORPTION(5,1)|CO2 FIXATION(5,1)|COARSE AGGREGATE ASTM(5,1)|COARSE AGGREGATE FRACTION(5,1)|COMBUSTION FLY ASH(5,1)|COMPACTED FILL(5,1)|CONCRETE AGGREGATE LIMIT(5,1)|CRYOGENIC SEPARATION(5,1)|EXHAUST STACK(5,1)|EXPERIMENTAL OVERVIEW(5,1)|FINE BUBBLE(5,1)|FRIABLE PARTICLE STANDARD(5,1)|GEOLOGICAL MEDIA(5,1)|INTAKE HOSE(5,1)|METHANE REPLACEMENT(5,1)|METHANEDIONE(5,1)|MORTAR MIX(5,1)|NITROGEN NOX REDUCTION TREATMENT(5,1)|PHENOLPHTHALEIN INDICATOR SOLUTION(5,1)|PRECOMBUSTION SEPARATION(5,1)|PREFOAMING SOLUTION EXPANSION(5,1)|REGULATOR FITTING(5,1)|RILEM TEST(5,1)|RUBBER HOSE EXTENSION(5,1)|SAMPLE CARBONATION(5,1)|TRADE NAME MEARLCRETE(5,1)|WET UNLOADER(5,1)|COLD WINTER(4,4)|GEOGRAPHIC LOCATION(4,4)|RXN(4,4)|BIOMASS(4,2)|COMMENT(4,2)|COMMITTEE(4,2)|COMPRESSOR(4,2)|CURING ROOM(4,2)|DISPOSAL(4,2)|GRADE STREAM HEAT(4,2)|METRIC TON(4,2)|ADVANCEMENT CATALYST(4,1)|AMMONIA MANUFACTURING(4,1)|ANALYSIS PARAMETER(4,1)|CARBON RICH FEEDSTOCK(4,1)|CEMENT MANUFACTURING(4,1)|CO2 SEPARATION(4,1)|COAL COMBUSTION CHAMBER(4,1)|COHESION(4,1)|CURED MASS(4,1)|CYLINDRICAL TEST SPECIMEN(4,1)|ENHANCE CO2(4,1)|ENVIRONMENTAL RESEARCH FACILITY(4,1)|ESTIMATION CALCULATION(4,1)|FLUE GAS GLOBULE(4,1)|FOAM NOZZLE(4,1)|FOSSIL FUEL BURNING PLANT(4,1)|FROTH CONCENTRATE SOLUTION(4,1)|FURNACE LOCATION(4,1)|INORGANIC MATRIX(4,1)|INORGANIC PARTICLE(4,1)|LOOSE PARTICLE(4,1)|MAINTENANCE GATE(4,1)|METHANEDIONE GAS(4,1)|METHANEDIONE SOURCE(4,1)|NONPHOTOSYNTHETIC(4,1)|OIL DEPLETION(4,1)|OXY FUEL COMBUSTION(4,1)|PUMICE FINE(4,1)|REDUCING METHANEDIONE PRODUCTION(4,1)|REMAINDER NITROGEN(4,1)|RUNNING MIXER(4,1)|TANK FILLING(4,1)|TERRESTRIAL ECOSYSTEM(4,1)|UNBURNED CARBON(4,1)|MIXTURE NUMBER(3,11)|FOAM VOLUME(3,3)|MAGNESIA(3,3)|FINAL CURED PRODUCT(3,2)|ACETOGENESIS(3,1)|ADVANCED CHEMICAL(3,1)|AERATED CONCRETE PRODUCT(3,1)|BACKFILL(3,1)|BASIC MIXTURE(3,1)|BIOLOGICAL SEQUESTRATION(3,1)|BLENDER(3,1)|BRIQUETTER(3,1)|CA REACTION(3,1)|CARBON PARTICLE(3,1)|CELLULAR CONCRETE STRUCTURE(3,1)|CEMENTITIOUS MATERIAL HYDRATION(3,1)|CO2 PRODUCTION(3,1)|CO2 REMOVAL(3,1)|CO2 SEQUESTRATION(3,1)|COMPACTION(3,1)|CONCRETE CONSTRUCTION YEAR(3,1)|ELASTIC FILM(3,1)|ELECTROSTATIC PRECIPITATOR(3,1)|ELEMENTAL MERCURY(3,1)|FEASIBILITY(3,1)|FERMENTATION(3,1)|FINAL MIXTURE PROPORTION(3,1)|FLOOR SLAB INTERIOR(3,1)|FLUE GAS CONTEXT(3,1)|FOAM PRODUCTION(3,1)|FOOTING(3,1)|FOREST(3,1)|FOUNDATION(3,1)| (US9028607)|What is claimed is:|1. A process for preparing a controlled low-strength material having a compressive strength of 1200 psi or less, the process comprising:| preparing a mixture including water and a cementitious material, wherein the cementitious material is selected from the group consisting of cement-kiln dust, lime-kiln dust, and slag cement;| recovering exhaust gas from a combustion chamber, wherein the exhaust gas includes carbon dioxide;| forming a foam including a foaming agent and the exhaust gas;| mixing the foam into the mixture to form a foamed mixture; and| thereafter allowing the foamed mixture to set to form the controlled low-strength material,| wherein during the step of allowing the foamed mixture to set, the carbon dioxide in the exhaust gas reacts with hydration products in the controlled low-strength material to sequester carbon dioxide.|2. The process of claim 1 wherein:| coal is combusted in the combustion chamber.|3. The process of claim 1 wherein:| the controlled low-strength material has a compressive strength of 300 psi or less.|4. The process of claim 1 further comprising:| shaping the foamed mixture into aggregates before allowing the foamed mixture to set.|5. The process of claim 1 further comprising:| subjecting the foamed mixture to a shaping process selected from pelletizing, extruding and briquetting before allowing the foamed mixture to set.|6. The process of claim 1 further comprising:| crushing the controlled low-strength material after the controlled low-strength material has set.|7. The process of claim 6 further comprising:| separating the crushed controlled low-strength material into different particle size fractions.|8. The process of claim 1 wherein:| the step of allowing the foamed mixture to set includes passing a heated fluid over the foamed mixture.|9. The process of claim 1 wherein:| the cementitious material is cement-kiln dust.|10. The process of claim 9 wherein:| the foamed mixture includes 1100-1400 pounds of cement-kiln dust per cubic yard of the foamed mixture and 800 to 1100 pounds of water per cubic yard of the foamed mixture.|11. The process of claim 10 wherein:| the foamed mixture includes 5 to 60 cubic feet of foam per cubic yard of the foamed mixture.|12. The process of claim 1 wherein:| the cementitious material is lime-kiln dust.|13. The process of claim 12 wherein:| the foamed mixture includes 1400-1800 pounds of lime-kiln dust per cubic yard of the foamed mixture and 500 to 800 pounds of water per cubic yard of the foamed mixture.|14. The process of claim 13 wherein:| the foamed mixture includes 7 to 40 cubic feet of foam per cubic yard of the foamed mixture.|15. The process of claim 1 wherein:| the cementitious material is slag cement.|16. The process of claim 15 wherein:| the foamed mixture includes 1400-1800 pounds of slag cement per cubic yard of the foamed mixture and 500 to 800 pounds of water per cubic yard of the foamed mixture.|17. The process of claim 16 wherein:| the foamed mixture includes 10 to 40 cubic feet of foam per cubic yard of the foamed mixture.|18. A process for sequestering carbon dioxide from exhaust gas emitted from a combustion chamber, the process comprising:| forming a foam including a foaming agent and the exhaust gas;| mixing the foam with a mixture including a cementitious material, wherein the cementitious material is selected from the group consisting of cement-kiln dust, lime-kiln dust, and slag cement, to form a foamed mixture; and| allowing the foamed mixture to set,| wherein the mixture sets to a controlled low-strength material having a compressive strength of 1200 psi or less, and| wherein during the step of allowing the foamed mixture to set, the carbon dioxide in the exhaust gas reacts with hydration products in the controlled low-strength material to sequester carbon dioxide.|19. The process of claim 18 wherein:| the mixture includes water, and| the cementitious material is cement-kiln dust.|20. The process of claim 18 wherein:| the mixture includes water, and| the cementitious material is lime-kiln dust.|21. The process of claim 18 wherein:| the mixture includes water, and| the cementitious material is slag cement.|22. A process for sequestering carbon dioxide from a gas including one weight percent or more carbon dioxide, the process comprising:| forming a foam including a foaming agent and the gas;| mixing the foam with a mixture including water and a material selected from the group consisting of cement-kiln dust, lime-kiln dust, and slag cement, to form a foamed mixture; and| allowing the foamed mixture to set to a controlled low-strength material having a compressive strength of 1200 psi or less,| wherein during the step of allowing the foamed mixture to set, the carbon dioxide in the exhaust gas reacts with hydration products in the controlled low-strength material to sequester carbon dioxide.|23. The process of claim 1 further comprising:| feeding the flue gas to a compressor to compress the flue gas to a higher pressure prior to forming the foam, the compressed exhaust gas being used to expand the foaming agent during the forming of the foam.|24. The process of claim 18 further comprising:| feeding the flue gas to a compressor to compress the flue gas to a higher pressure prior to forming the foam, the compressed exhaust gas being used to expand the foaming agent during the forming of the foam.|25. The process of claim 22 further comprising:| feeding the flue gas to a compressor to compress the flue gas to a higher pressure prior to forming the foam, the compressed exhaust gas being used to expand the foaming agent during the forming of the foam. (US9028607)|CROSS-REFERENCES TO RELATED APPLICATIONS|[0001] This application is a continuation-in-part of U.S. patent application Ser. No. 11/064,756, filed Feb. 24, 2005 now U.S. Pat. No. 7,390,444, which is incorporated herein by reference.|(US9028607)|STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH|[0002] Not Applicable.|BACKGROUND OF THE INVENTION|[0003] 1. Field of the Invention|[0004] This invention relates to a process for sequestering carbon dioxide through the production of lightweight controlled low-strength materials.|[0005] 2. Description of the Related Art|[0006] Man made carbon dioxide (CO2) has been viewed by some as being a pollutant. There are many sources of CO2 including power plants, cement manufacturing, lime manufacturing, iron production, vehicles, natural gas ensuing from wells, ammonia manufacturing, fermentation, hydrogen production (e.g., in oil refining), and producing hydrogen fuels from carbon-rich feedstocks, such as natural gas, coal, and biomass. Thus, there has been interest in processes for sequestering carbon dioxide.|[0007] Permanent sequestration of carbon dioxide can occur by terrestrial ecosystems. For example, in forests and trees, 74,806 metric tons of carbon dioxide can be sequestered per 1,000-acre plantation in seven years. Also, grasses and prairies, such as the United States Great Plains, sequester 740 kg/ha/year. Agricultural and biomass croplands, boreal wetlands and peatlands in United States agricultural lands sequester carbon dioxide at rates of 75-200 million metric tons per year.|[0008] Permanent sequestration of CO2 can also occur by advanced chemical and biological sequestration wherein CO2 is converted into either commercial products that are inert and long lived or that are stable solid compounds. Examples include: magnesium carbonate, CO2 ice-like material, advanced catalysts for CO2 and CO conversion, engineered photosynthesis systems, non-photosynthetic mechanisms for CO2 fixation (methanogenesis and acetogenesis), genetic manipulation of agriculture and forests to enhance CO2 sequestering potential, advanced decarbonization systems, and biomimetic systems.|[0009] Permanent sequestration of carbon dioxide also occurs by the natural carbonation of concrete. About 0.2 pounds of carbon dioxide is absorbed per 1 pound of cement in concrete over time. During a typical year of concrete construction in the United States, 274,000 metric tons of atmospheric CO2 are absorbed. Over a 100-year period, all of the concrete produced during a single typical year will absorb 2,906,000 metric tons.|[0010] Various methods are known for storing carbon dioxide in geological media such as enhanced oil recovery, storage in depleted oil and gas reservoirs, replacement of methane by carbon dioxide in deep coal beds, injection into deep saline aquifers, and storage in salt caverns. Also, ocean sequestration of carbon dioxide is known. Carbon dioxide may be stored underwater in large canyons or injected directly into the deep ocean, via pipeline or tanker. Furthermore, oceans naturally sequester carbon dioxide. It has also been proposed to capture carbon dioxide by microalgae, ocean fertilization, or non-biological capture from the air.|[0011] Of course, various methods for reducing carbon dioxide production are also known. For example, power plant efficiency can be increased by way of: (i) processes, such as flue gas separation, oxy-fuel combustion, and pre-combustion separation, and (ii) systems, such as solvents (chemical, physical, and hybrid systems), membranes, cryogenic separation, solid-bed adsorbents, and combined systems. Carbon dioxide production can also be reduced by decreased manufacturing of cement through use of alternatives to conventional cement like fly ash. Decreased use of vehicles can also reduce carbon dioxide production.|[0012] It has been reported that in 2000, carbon dioxide emissions reached 5.8 billion metric tons and that approximately 80% of annual emissions come from the burning of fossil fuels. Therefore, there have been efforts to limit man made carbon dioxide emissions from fossil fuel burning plants. U.S. Pat. No. 6,235,092 provides a discussion of a variety of processes that have been developed for removing a gaseous component (such as carbon dioxide) from a multicomponent gaseous stream (such as the exhaust gas stream of a coal burning electrical power generation plant). Selective adsorption by solid adsorbents and gas absorption are named as two example processes. This patent further mentions that gas absorption finds use in the separation of CO2 from multicomponent gaseous streams. It is reported that in some CO2 gas absorption processes, the following steps are employed: (1) absorption of CO2 from the gaseous stream by a host solvent such as monoethanolamine; (2) removal of CO2 from the host solvent by steam stripping; and (3) compression of the stripped CO2 for disposal such as by sequestration through deposition in the deep ocean or ground aquifers. Other patents describing CO2 sequestration methods include U.S. Pat. Nos. 6,648,949, 6,372,023 and 5,397,553.|[0013] Although these processes may be successful in sequestering carbon dioxide, they can be energy intensive. Thus, there is continued interest in the development of less energy intensive processes for sequestering carbon dioxide from the exhaust gas streams of industrial and power generation plants.|[0014] It is also known that cement-kiln dust, lime-kiln dust, and slag cement are voluminous cementitious by-products of industry, presenting air quality and environmental disposal issues. Cement-kiln dust is a by-product of the manufacture of portland cement, and nearly 4 million tons of cement kiln dust are disposed of every year in the United States. Maintaining cement-kiln dust landfills is expensive and difficult because of the fine, dusty nature of the material, and disposal costs add significantly to the cost of cement manufacture. Cement manufacturers are making efforts to minimize the generation of cement kiln dust and to develop alternative uses for this material.|[0015] Lime-kiln dust is a by-product of the manufacture of lime in a rotary kiln. Lime-kiln dust has limited use as a raw material in cement production and is commonly used in agriculture as a soil stabilizer or soil-modifying agent. As with cement-kiln dust, manufacturers are making efforts to reduce disposal costs and environmental impact by minimizing the generation of lime-kiln dust and developing alternative uses for the material.|[0016] Slag cement is a by-product of iron production. When mixed with portland cement, it is used in concrete and other construction applications. The use of slag cement in concrete and cement mixes has economic and environmental benefits, reducing slag disposal costs, greenhouse gas emissions, and total energy use.|[0017] Controlled low-strength materials are described in the publication “Controlled Low-Strength Materials”, reported by American Concrete Institute Committee 229, June 1999, as self-compacted, cementitious materials used primarily as a backfill in place of compacted fill. Conventional CLSM mixtures consist of water, portland cement, fly ash, and, optionally, additional fine or coarse aggregates. However, CLSM mixtures can be made of other cementitious materials mixed with water. This publication defines CLSM as a material that results in a compressive strength of 8.3 MPa (1200 psi) or less at the conventional 28 day testing period (typically without compaction), and notes that most current CLSM applications require unconfined compressive strengths of 2.1 MPa (300 psi) or less at the conventional 28 day testing period in order to allow future excavation. The use of cement-kiln dust, lime-kiln dust, and/or slag cement in CLSM provides a environmentally beneficial use for these cementitious materials.|[0018] It is also known that the density of cement-containing materials can be lowered by entraining gas in the materials. For example, U.S. Pat. No. 3,867,159 describes cellular concrete structures made by mixing water and cement followed by the introduction of a foam produced by a foam generator. U.S. Pat. No. 4,383,862 discloses a method of producing aerated concrete wherein a gas such as air, carbon dioxide, or a mixture thereof is introduced into a blender with a mortar mix. U.S. Pat. No. 5,654,352 describes air-entraining agents for use in cementitious mixtures. Some of these mixtures are reported as being controlled low-strength materials. U.S. Pat. Nos. 6,153,005, 5,013,157, 4,900,359, 4,415,366 and 4,407,676 describe related processes.|[0019] It is also known that the hardening of cement-containing materials can be accelerated by carbonation in which calcium hydroxide in the cement is transformed into calcium carbonate by absorbing carbon dioxide. Related processes are described in U.S. Pat. Nos. 6,387,174, 6,264,736, 5,965,201, 5,897,704, 5,690,729, 5,650,562, 5,518,540, 5,307,876, 5,051,217, 4,427,610, 4,362,679, 4,350,567, 4,117,060, 4,093,690 and 4,069,063, German patent application DE 4207235, Swiss patent application CH 644828, and Japanese patent applications JP 6263562 and JP 2018368.|[0020] There is a continuing need to safely and economically dispose of such industrial by-products as cement-kiln dust, lime-kiln dust, and slag cement; thus, there is a continuing need for products and processes that make environmentally beneficial use of these by-products. In addition, increasing global concerns regarding greenhouse gas emissions have created a continuing need for products and processes that permanently remove free carbon dioxide from the environment.|SUMMARY OF THE INVENTION|[0021] The foregoing needs are met by a process according to the invention for sequestering carbon dioxide from the flue gas emitted from a combustion chamber such as that included in a fossil fuel burning power plant, a cement kiln, a lime kiln, or a blast furnace. In the process, a foam including a foaming agent and the flue gas is formed, and the foam is added to a mixture including a cementitious material (e.g., cement-kiln dust, lime-kiln dust, or slag cement) to form a foamed mixture. Thereafter, the foamed mixture is allowed to set, preferably to a controlled low-strength material having a compressive strength of 1200 psi or less.|[0022] In the process, the normal air used in producing the foam is replaced with carbon dioxide and flue gas generated from the electric power or industrial production plant. The carbon dioxide in the flue gas reacts with hydration products in the controlled low-strength material and in turn sequesters the carbon dioxide. In a typical material, carbonation occurs at the surface, where the material is exposed to a source of carbon dioxide, for example from air, and slowly penetrates further in depth. In contrast, lightweight foamed controlled low-strength materials are particularly suitable to increase the surface area exposed to carbon dioxide. In the foamed controlled low-strength material of the present invention, there are millions of air bubbles that contain carbon dioxide, so there can be an almost unlimited amount of surface area of controlled low-strength material where carbonation may occur. In the process, the compressive strength of the controlled low-strength material increases due to the carbonation. Also advantageously, the man made carbon dioxide emissions from a fossil fuel burning plant are decreased by sequestration of the carbon dioxide in the foamed controlled low-strength material.|[0023] Carbonation occurs when part of the calcium hydroxide formed during hydration of cementitious materials containing calcium oxide, such as cement-kiln dust, lime-kiln dust, or slag cement, combines in the course of hardening with the carbon dioxide and produces calcium carbonate in the following chemical reaction.|Ca(OH)2+CO2→CaCO3+H2O|Calcium Hydroxide+Carbon Dioxide→Calcium Carbonate+Water|[0024] Cement-kiln dust, lime-kiln dust, and slag cement all contain substantial amounts of calcium oxide. When hydrated with water, the calcium oxide is converted to calcium hydroxide. Thus, when a controlled low-strength material mixture of any of those materials and water is made, there is a sufficient quantity of calcium hydroxide present for the carbonation reaction to occur, and for concurrently sequestering free carbon dioxide and increasing the compressive strength of the controlled low-strength material.|[0025] It should be appreciated that the process of the invention is not limited to sequestering carbon dioxide from the flue gas emitted from a combustion chamber. The process may be used to sequester carbon dioxide from other mixed gases including carbon dioxide. Also, other exhaust gases can be used in the process. For example, other fossil fuel combustion gas from related industrial processes (such as kiln exhaust or blast furnace exhaust gas) are suitable for use in the process. All are a result of fossil fuel combustion and contain CO2 and useful residual heat for curing in winter climates.|[0026] It is therefore an advantage of the present invention to provide products and processes that make environmentally beneficial use of the carbon dioxide, cement-kiln dust, lime-kiln dust, and slag cement produced as by-products of fossil fuel burning power plants and industrial production plants.|[0027] These and other features, aspects, and advantages of the present invention will become better understood upon consideration of the following detailed description, drawings, and appended claims.|(US9028607)|BRIEF DESCRIPTION OF THE DRAWINGS|[0028] FIG. 1 is a schematic showing an example process according to the invention.|(US9028607)|DETAILED DESCRIPTION OF THE INVENTION|[0029] Turning to FIG. 1, there is shown an example process according to the invention. In a first step, flue gas is removed from a combustion chamber such as that of a coal-fired power plant or cement kiln. The flue gas source may be an exhaust stack or other convenient furnace location where flue gas is emitted from the combustion chamber. While the example process is typically used in the context of flue gas generated by a coal-fired power plant, it is not limited to such applications.|[0030] In general, coal-fired power plant flue gas may include fly ash, nitrogen, oxygen, carbon dioxide, nitrogen oxides, water, carbon monoxide, sulfur oxides, mercury, and various acid gases. The precise composition of the flue gas is determined by the nature of the process generating the flue gas and can vary significantly in time. In studies reported in U.S. Pat. No. 6,521,021, the United States Combustion Environmental Research Facility operates a pulverized coal combustion unit that simulates the firing of a utility power plant and that produces a simulated flue gas containing 16% carbon dioxide, 5% oxygen, 2000 ppm sulfur dioxide, 500 ppm nitric oxide, 270 ppb elemental mercury, and the remainder nitrogen.|[0031] In a second step of the process of the invention, the flue gas is fed via a conduit to a compressor where the flue gas is compressed to a higher pressure. One example pressure after compression is 100 psi, although the invention is not limited to that pressure.|[0032] Still referring to FIG. 1, the compressed flue gas is then fed via a conduit to a foam generator. A typical foam generator will include an input for water, an input for a foaming agent, and an input for the compressed flue gas which arrives via the conduit from the compressor. Foam generators are commercially available, and example suppliers include Elastizell Corporation of America, Ann Arbor, Mich., USA, and Cellular Concrete LLC, Roselle Park, N.J., USA. The foaming agent is typically a soap or a surfactant. Foaming agents are also commercially available, and one example supplier is Elastizell. Another example supplier is Cellular Concrete LLC, which sells aqueous surface-active polypeptide-alkylene polyol condensate foaming agents under the trade names Mearicrete® and Geofoam™.|[0033] The foam generator mixes the water and the foaming agent in a selectable ratio to form a pre-foaming solution. The compressed flue gas and the pre-foaming solution are then fed through an exit conduit of the foam generator which creates a foam by expansion of the pre-foaming solution with the gas. By “foam” herein, we mean a dispersion of gas in a liquid solution. The flue gas globules may be of any size from colloidal to macroscopic. The pre-foaming solution must have sufficient cohesion to form an elastic film. While the preferred foam generator produces a mechanical foam (i.e., a foam produced by mixing gas with water containing a foaming agent), chemical foams (i.e., foams produced by a chemical reaction that produces gas) could supplement the mechanical foam. The foam generator may be specially manufactured to handle a large scale process. The use of the generated foam will be described further below.|[0034] Referring still to FIG. 1, in a separate process step, cement-kiln dust, lime kiln dust, and/or slag cement are obtained. Cement-kiln dust, commonly referred to as CKD, is a by-product captured from the hot gasses in dust collectors during the manufacture of portland cement. It is collected during the cement manufacturing process in a dust collecting and recycling baghouse. CKD differs from portland cement in that the raw ingredients added in a kiln to produce cement may not have been fully burned. CKD consists mainly of calcium, silica, and aluminum oxides along with smaller quantities of calcium sulfate, potassium oxides, sodium oxides, and metals derived from the raw ingredients utilized in cement manufacturing, which include limestone and clay, and sometimes may include slate, fly ash, and slag.|[0035] CKD generally has a specific gravity around 2.8 and a maximum dry density of 1,520 kg/m3. The maximum particle size of CKD is typically 0.3 mm (No. 50 sieve) and often 75% of the material passes through a 0.03 mm (No. 450 sieve) opening. The amount and compound form of calcium oxide and amount of free lime available from CKD varies between the cement manufacturing facilities.|[0036] Lime-kiln dust is commonly referred to as LKD and is a by-product of lime manufacturing in a rotary kiln. Limestone (usually primarily consisting of calcium carbonate) is heated in the kiln, which drives off carbon dioxide and forms lime (calcium oxide). LKD is collected from hot gasses in dust collectors and can vary chemically depending on the type of limestone being used. The available CaO content can range typically from 20 to 40%. LKD is mainly calcium oxide but contains varying amounts of magnesium oxide if dolomitic limestone is used, calcium sulfate depending on the sulfur content of the kiln fuel, fly ash when coal is used as the fuel, and dust from limestone handling and unburned limestone. Other impurities such as silica, iron, aluminum, and other metals may also be present, but in very small amounts, because the limestone used for the manufacture of lime is typically quite pure to meet chemical standards. LKD differs from commercial lime in that the raw ingredients in LKD have not been fully burned.|[0037] LKD has a specific gravity that typically falls between 2.4 and 3.0 and a bulk density that falls between 720-1150 kg/m3. The particle size range of LKD falls between 0.005 mm and 2.0 mm and generally 75% of the material passes through a 0.03 mm (No. 450 sieve). The amount of calcium oxide and amount of free-lime present in LKD varies between lime manufacturing facilities depending on the source of the limestone and kiln process used.|[0038] Slag cement (also called ground granulated blast furnace slag) is a hydraulic cement produced during the reduction of iron ore to iron in a blast furnace. Molten slag is tapped from a blast furnace, rapidly quenched with water (“granulated”), dried, and ground to a fine powder. The rapid quenching ‘freezes’ the molten slag in a glassy state, which gives the product its cementitious properties.|[0039] When iron is manufactured using a blast furnace, the furnace is continuously charged from the top with oxides, fluxing material, and fuel. Two products—slag and iron—collect in the bottom of the hearth. Molten slag floats on top of the molten iron; both are tapped separately. The molten iron is sent to the steel producing facility, while the molten slag is diverted to a granulator. This process, known as granulation, is the rapid quenching with water of the molten slag into a raw material called granules. Rapid cooling prohibits the formation of crystals and forms glassy, non-metallic, silicates and alumino-silicates of calcium. These granules are dried and then ground to a suitable fineness, the result of which is the slag cement. The granules can also be incorporated as an ingredient in the manufacture of blended portland cement. Slag cement (ground granulated blast furnace slag) typically has a specific gravity that falls between 2.85 and 2.94, and consists of about 45% CaO, 33% SiO2, 10% Al2O3, 1% Fe2O3, and 6% MgO.|[0040] In a next process step of FIG. 1, cement-kiln dust, lime kiln dust, and/or slag cement are combined with foam from the foam generator and water in a mixer (wet unloader) to form a foamed mixture. Various foamed mixtures of the cementitious material, foam and water are possible. In one specific embodiment, the foamed mixture includes about 1275 pounds of cement-kiln dust per cubic yard of the foamed mixture and about 960 pounds of water per cubic yard of the foamed mixture. In another specific embodiment, the foamed mixture includes about 1575 pounds of lime-kiln dust per cubic yard of the foamed mixture and about 660 pounds of water per cubic yard of the foamed mixture. In a third specific embodiment, the foamed mixture includes about 1600 pounds of slag cement per cubic yard of the foamed mixture and about 650 pounds of water per cubic yard of the foamed mixture. These specific embodiments are not limiting in the possible proportions of cementitious material, water, and foam that could be used in the foamed mixture. Also, an over dosage of foam is beneficial in certain cases because of the instability/breakdown of the foam during mixing.|[0041] In addition to cement-kiln dust, lime kiln dust, or slag cement, other cementitious materials may also be used in the foamed mixture. Examples of other cementitious materials that could be added include portland cement and fly ash. It is also contemplated that other materials, such as fine aggregate and coarse aggregate, may be included in the foamed mixture. However, in certain embodiments, the foamed mixture may consist essentially of water, cement-kiln dust and foam; water, lime-kiln dust and foam; or water, slag cement and foam. This avoids the need to integrate other materials into the foamed mixture that may affect properties of the final cured product.|[0042] After the foamed mixture is prepared, different process steps may be undertaken. In Option #1 of FIG. 1, the foamed mixture is removed from the mixer and loaded onto a vehicle that transports the foamed mixture to a curing station where the foamed mixture sets. In geographic locations where cold winters are experienced, the foamed mixture may be transported to a curing station in the power plant building or to a below ground silo/bin. In order to accelerate curing/setting of the foamed mixture, flue gas and/or low grade stream heat, preferably recovered from the power plant, are passed over and/or through the foamed mixture. During the summer season, or in geographic locations where cold winters are not experienced, the foamed mixture may be transported to an outdoor storage pile for curing/setting of the foamed mixture.|[0043] During curing/setting of the foamed mixture, the carbon dioxide in the flue gas dispersed in the foaming agent reacts with hydration products in the foamed mixture and in turn sequesters the carbon dioxide. The cured/set foamed mixture typically meets the standards for controlled low-strength materials as published by the American Concrete Institute. For example, the process of the invention produces a controlled low-strength material that results in a compressive strength of 8.3 MPa (1200 psi) or less at the conventional 28 day testing period, and may produce a controlled low-strength material with unconfined compressive strengths of 2.1 MPa (300 psi) or less at the conventional 28 day testing period.|[0044] Referring still to FIG. 1, after curing/setting of the foamed mixture, the cured mass may be crushed into aggregate and thereafter screened into an undersize fine aggregate fraction and a coarse aggregate fraction that meets a predetermined coarse aggregate material specification such as those published by the American Society for Testing and Materials.|[0045] In Option #2 of FIG. 1, the foamed mixture is removed from the mixer and fed to a shaping device such as a pan pelletizer, extruder or briquetter for shaping into aggregate. In geographic locations where cold winters are experienced, the shaped aggregate is conveyed to a curing station in the power plant building or to a below ground silo/bin. In order to accelerate curing/setting of the shaped aggregate, flue gas and/or low grade stream heat, preferably recovered from the power plant, are passed over and/or through the shaped aggregate. During the summer season, or in geographic locations where cold winters are not experienced, the shaped aggregate may be transported to an outdoor storage pile for curing/setting of the shaped aggregate. (US9028607)|CROSS-REFERENCES TO RELATED APPLICATIONS|[0001] This application is a continuation-in-part of U.S. patent application Ser. No. 11/064,756, filed Feb. 24, 2005 now U.S. Pat. No. 7,390,444, which is incorporated herein by reference.|(US9028607)|STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH|[0002] Not Applicable.|BACKGROUND OF THE INVENTION|[0003] 1. Field of the Invention|[0004] This invention relates to a process for sequestering carbon dioxide through the production of lightweight controlled low-strength materials.|[0005] 2. Description of the Related Art|[0006] Man made carbon dioxide (CO2) has been viewed by some as being a pollutant. There are many sources of CO2 including power plants, cement manufacturing, lime manufacturing, iron production, vehicles, natural gas ensuing from wells, ammonia manufacturing, fermentation, hydrogen production (e.g., in oil refining), and producing hydrogen fuels from carbon-rich feedstocks, such as natural gas, coal, and biomass. Thus, there has been interest in processes for sequestering carbon dioxide.|[0007] Permanent sequestration of carbon dioxide can occur by terrestrial ecosystems. For example, in forests and trees, 74,806 metric tons of carbon dioxide can be sequestered per 1,000-acre plantation in seven years. Also, grasses and prairies, such as the United States Great Plains, sequester 740 kg/ha/year. Agricultural and biomass croplands, boreal wetlands and peatlands in United States agricultural lands sequester carbon dioxide at rates of 75-200 million metric tons per year.|[0008] Permanent sequestration of CO2 can also occur by advanced chemical and biological sequestration wherein CO2 is converted into either commercial products that are inert and long lived or that are stable solid compounds. Examples include: magnesium carbonate, CO2 ice-like material, advanced catalysts for CO2 and CO conversion, engineered photosynthesis systems, non-photosynthetic mechanisms for CO2 fixation (methanogenesis and acetogenesis), genetic manipulation of agriculture and forests to enhance CO2 sequestering potential, advanced decarbonization systems, and biomimetic systems.|[0009] Permanent sequestration of carbon dioxide also occurs by the natural carbonation of concrete. About 0.2 pounds of carbon dioxide is absorbed per 1 pound of cement in concrete over time. During a typical year of concrete construction in the United States, 274,000 metric tons of atmospheric CO2 are absorbed. Over a 100-year period, all of the concrete produced during a single typical year will absorb 2,906,000 metric tons.|[0010] Various methods are known for storing carbon dioxide in geological media such as enhanced oil recovery, storage in depleted oil and gas reservoirs, replacement of methane by carbon dioxide in deep coal beds, injection into deep saline aquifers, and storage in salt caverns. Also, ocean sequestration of carbon dioxide is known. Carbon dioxide may be stored underwater in large canyons or injected directly into the deep ocean, via pipeline or tanker. Furthermore, oceans naturally sequester carbon dioxide. It has also been proposed to capture carbon dioxide by microalgae, ocean fertilization, or non-biological capture from the air.|[0011] Of course, various methods for reducing carbon dioxide production are also known. For example, power plant efficiency can be increased by way of: (i) processes, such as flue gas separation, oxy-fuel combustion, and pre-combustion separation, and (ii) systems, such as solvents (chemical, physical, and hybrid systems), membranes, cryogenic separation, solid-bed adsorbents, and combined systems. Carbon dioxide production can also be reduced by decreased manufacturing of cement through use of alternatives to conventional cement like fly ash. Decreased use of vehicles can also reduce carbon dioxide production.|[0012] It has been reported that in 2000, carbon dioxide emissions reached 5.8 billion metric tons and that approximately 80% of annual emissions come from the burning of fossil fuels. Therefore, there have been efforts to limit man made carbon dioxide emissions from fossil fuel burning plants. U.S. Pat. No. 6,235,092 provides a discussion of a variety of processes that have been developed for removing a gaseous component (such as carbon dioxide) from a multicomponent gaseous stream (such as the exhaust gas stream of a coal burning electrical power generation plant). Selective adsorption by solid adsorbents and gas absorption are named as two example processes. This patent further mentions that gas absorption finds use in the separation of CO2 from multicomponent gaseous streams. It is reported that in some CO2 gas absorption processes, the following steps are employed: (1) absorption of CO2 from the gaseous stream by a host solvent such as monoethanolamine; (2) removal of CO2 from the host solvent by steam stripping; and (3) compression of the stripped CO2 for disposal such as by sequestration through deposition in the deep ocean or ground aquifers. Other patents describing CO2 sequestration methods include U.S. Pat. Nos. 6,648,949, 6,372,023 and 5,397,553.|[0013] Although these processes may be successful in sequestering carbon dioxide, they can be energy intensive. Thus, there is continued interest in the development of less energy intensive processes for sequestering carbon dioxide from the exhaust gas streams of industrial and power generation plants.|[0014] It is also known that cement-kiln dust, lime-kiln dust, and slag cement are voluminous cementitious by-products of industry, presenting air quality and environmental disposal issues. Cement-kiln dust is a by-product of the manufacture of portland cement, and nearly 4 million tons of cement kiln dust are disposed of every year in the United States. Maintaining cement-kiln dust landfills is expensive and difficult because of the fine, dusty nature of the material, and disposal costs add significantly to the cost of cement manufacture. Cement manufacturers are making efforts to minimize the generation of cement kiln dust and to develop alternative uses for this material.|[0015] Lime-kiln dust is a by-product of the manufacture of lime in a rotary kiln. Lime-kiln dust has limited use as a raw material in cement production and is commonly used in agriculture as a soil stabilizer or soil-modifying agent. As with cement-kiln dust, manufacturers are making efforts to reduce disposal costs and environmental impact by minimizing the generation of lime-kiln dust and developing alternative uses for the material.|[0016] Slag cement is a by-product of iron production. When mixed with portland cement, it is used in concrete and other construction applications. The use of slag cement in concrete and cement mixes has economic and environmental benefits, reducing slag disposal costs, greenhouse gas emissions, and total energy use.|[0017] Controlled low-strength materials are described in the publication “Controlled Low-Strength Materials”, reported by American Concrete Institute Committee 229, June 1999, as self-compacted, cementitious materials used primarily as a backfill in place of compacted fill. Conventional CLSM mixtures consist of water, portland cement, fly ash, and, optionally, additional fine or coarse aggregates. However, CLSM mixtures can be made of other cementitious materials mixed with water. This publication defines CLSM as a material that results in a compressive strength of 8.3 MPa (1200 psi) or less at the conventional 28 day testing period (typically without compaction), and notes that most current CLSM applications require unconfined compressive strengths of 2.1 MPa (300 psi) or less at the conventional 28 day testing period in order to allow future excavation. The use of cement-kiln dust, lime-kiln dust, and/or slag cement in CLSM provides a environmentally beneficial use for these cementitious materials.|[0018] It is also known that the density of cement-containing materials can be lowered by entraining gas in the materials. For example, U.S. Pat. No. 3,867,159 describes cellular concrete structures made by mixing water and cement followed by the introduction of a foam produced by a foam generator. U.S. Pat. No. 4,383,862 discloses a method of producing aerated concrete wherein a gas such as air, carbon dioxide, or a mixture thereof is introduced into a blender with a mortar mix. U.S. Pat. No. 5,654,352 describes air-entraining agents for use in cementitious mixtures. Some of these mixtures are reported as being controlled low-strength materials. U.S. Pat. Nos. 6,153,005, 5,013,157, 4,900,359, 4,415,366 and 4,407,676 describe related processes.|[0019] It is also known that the hardening of cement-containing materials can be accelerated by carbonation in which calcium hydroxide in the cement is transformed into calcium carbonate by absorbing carbon dioxide. Related processes are described in U.S. Pat. Nos. 6,387,174, 6,264,736, 5,965,201, 5,897,704, 5,690,729, 5,650,562, 5,518,540, 5,307,876, 5,051,217, 4,427,610, 4,362,679, 4,350,567, 4,117,060, 4,093,690 and 4,069,063, German patent application DE 4207235, Swiss patent application CH 644828, and Japanese patent applications JP 6263562 and JP 2018368.|[0020] There is a continuing need to safely and economically dispose of such industrial by-products as cement-kiln dust, lime-kiln dust, and slag cement; thus, there is a continuing need for products and processes that make environmentally beneficial use of these by-products. In addition, increasing global concerns regarding greenhouse gas emissions have created a continuing need for products and processes that permanently remove free carbon dioxide from the environment.|SUMMARY OF THE INVENTION|[0021] The foregoing needs are met by a process according to the invention for sequestering carbon dioxide from the flue gas emitted from a combustion chamber such as that included in a fossil fuel burning power plant, a cement kiln, a lime kiln, or a blast furnace. In the process, a foam including a foaming agent and the flue gas is formed, and the foam is added to a mixture including a cementitious material (e.g., cement-kiln dust, lime-kiln dust, or slag cement) to form a foamed mixture. Thereafter, the foamed mixture is allowed to set, preferably to a controlled low-strength material having a compressive strength of 1200 psi or less.|[0022] In the process, the normal air used in producing the foam is replaced with carbon dioxide and flue gas generated from the electric power or industrial production plant. The carbon dioxide in the flue gas reacts with hydration products in the controlled low-strength material and in turn sequesters the carbon dioxide. In a typical material, carbonation occurs at the surface, where the material is exposed to a source of carbon dioxide, for example from air, and slowly penetrates further in depth. In contrast, lightweight foamed controlled low-strength materials are particularly suitable to increase the surface area exposed to carbon dioxide. In the foamed controlled low-strength material of the present invention, there are millions of air bubbles that contain carbon dioxide, so there can be an almost unlimited amount of surface area of controlled low-strength material where carbonation may occur. In the process, the compressive strength of the controlled low-strength material increases due to the carbonation. Also advantageously, the man made carbon dioxide emissions from a fossil fuel burning plant are decreased by sequestration of the carbon dioxide in the foamed controlled low-strength material.|[0023] Carbonation occurs when part of the calcium hydroxide formed during hydration of cementitious materials containing calcium oxide, such as cement-kiln dust, lime-kiln dust, or slag cement, combines in the course of hardening with the carbon dioxide and produces calcium carbonate in the following chemical reaction.|Ca(OH)2+CO2→CaCO3+H2O|Calcium Hydroxide+Carbon Dioxide→Calcium Carbonate+Water|[0024] Cement-kiln dust, lime-kiln dust, and slag cement all contain substantial amounts of calcium oxide. When hydrated with water, the calcium oxide is converted to calcium hydroxide. Thus, when a controlled low-strength material mixture of any of those materials and water is made, there is a sufficient quantity of calcium hydroxide present for the carbonation reaction to occur, and for concurrently sequestering free carbon dioxide and increasing the compressive strength of the controlled low-strength material.|[0025] It should be appreciated that the process of the invention is not limited to sequestering carbon dioxide from the flue gas emitted from a combustion chamber. The process may be used to sequester carbon dioxide from other mixed gases including carbon dioxide. Also, other exhaust gases can be used in the process. For example, other fossil fuel combustion gas from related industrial processes (such as kiln exhaust or blast furnace exhaust gas) are suitable for use in the process. All are a result of fossil fuel combustion and contain CO2 and useful residual heat for curing in winter climates.|[0026] It is therefore an advantage of the present invention to provide products and processes that make environmentally beneficial use of the carbon dioxide, cement-kiln dust, lime-kiln dust, and slag cement produced as by-products of fossil fuel burning power plants and industrial production plants.|[0027] These and other features, aspects, and advantages of the present invention will become better understood upon consideration of the following detailed description, drawings, and appended claims.|(US9028607)|BRIEF DESCRIPTION OF THE DRAWINGS|[0028] FIG. 1 is a schematic showing an example process according to the invention.|(US9028607)|DETAILED DESCRIPTION OF THE INVENTION|[0029] Turning to FIG. 1, there is shown an example process according to the invention. In a first step, flue gas is removed from a combustion chamber such as that of a coal-fired power plant or cement kiln. The flue gas source may be an exhaust stack or other convenient furnace location where flue gas is emitted from the combustion chamber. While the example process is typically used in the context of flue gas generated by a coal-fired power plant, it is not limited to such applications.|[0030] In general, coal-fired power plant flue gas may include fly ash, nitrogen, oxygen, carbon dioxide, nitrogen oxides, water, carbon monoxide, sulfur oxides, mercury, and various acid gases. The precise composition of the flue gas is determined by the nature of the process generating the flue gas and can vary significantly in time. In studies reported in U.S. Pat. No. 6,521,021, the United States Combustion Environmental Research Facility operates a pulverized coal combustion unit that simulates the firing of a utility power plant and that produces a simulated flue gas containing 16% carbon dioxide, 5% oxygen, 2000 ppm sulfur dioxide, 500 ppm nitric oxide, 270 ppb elemental mercury, and the remainder nitrogen.|[0031] In a second step of the process of the invention, the flue gas is fed via a conduit to a compressor where the flue gas is compressed to a higher pressure. One example pressure after compression is 100 psi, although the invention is not limited to that pressure.|[0032] Still referring to FIG. 1, the compressed flue gas is then fed via a conduit to a foam generator. A typical foam generator will include an input for water, an input for a foaming agent, and an input for the compressed flue gas which arrives via the conduit from the compressor. Foam generators are commercially available, and example suppliers include Elastizell Corporation of America, Ann Arbor, Mich., USA, and Cellular Concrete LLC, Roselle Park, N.J., USA. The foaming agent is typically a soap or a surfactant. Foaming agents are also commercially available, and one example supplier is Elastizell. Another example supplier is Cellular Concrete LLC, which sells aqueous surface-active polypeptide-alkylene polyol condensate foaming agents under the trade names Mearicrete® and Geofoam™.|[0033] The foam generator mixes the water and the foaming agent in a selectable ratio to form a pre-foaming solution. The compressed flue gas and the pre-foaming solution are then fed through an exit conduit of the foam generator which creates a foam by expansion of the pre-foaming solution with the gas. By “foam” herein, we mean a dispersion of gas in a liquid solution. The flue gas globules may be of any size from colloidal to macroscopic. The pre-foaming solution must have sufficient cohesion to form an elastic film. While the preferred foam generator produces a mechanical foam (i.e., a foam produced by mixing gas with water containing a foaming agent), chemical foams (i.e., foams produced by a chemical reaction that produces gas) could supplement the mechanical foam. The foam generator may be specially manufactured to handle a large scale process. The use of the generated foam will be described further below.|[0034] Referring still to FIG. 1, in a separate process step, cement-kiln dust, lime kiln dust, and/or slag cement are obtained. Cement-kiln dust, commonly referred to as CKD, is a by-product captured from the hot gasses in dust collectors during the manufacture of portland cement. It is collected during the cement manufacturing process in a dust collecting and recycling baghouse. CKD differs from portland cement in that the raw ingredients added in a kiln to produce cement may not have been fully burned. CKD consists mainly of calcium, silica, and aluminum oxides along with smaller quantities of calcium sulfate, potassium oxides, sodium oxides, and metals derived from the raw ingredients utilized in cement manufacturing, which include limestone and clay, and sometimes may include slate, fly ash, and slag.|[0035] CKD generally has a specific gravity around 2.8 and a maximum dry density of 1,520 kg/m3. The maximum particle size of CKD is typically 0.3 mm (No. 50 sieve) and often 75% of the material passes through a 0.03 mm (No. 450 sieve) opening. The amount and compound form of calcium oxide and amount of free lime available from CKD varies between the cement manufacturing facilities.|[0036] Lime-kiln dust is commonly referred to as LKD and is a by-product of lime manufacturing in a rotary kiln. Limestone (usually primarily consisting of calcium carbonate) is heated in the kiln, which drives off carbon dioxide and forms lime (calcium oxide). LKD is collected from hot gasses in dust collectors and can vary chemically depending on the type of limestone being used. The available CaO content can range typically from 20 to 40%. LKD is mainly calcium oxide but contains varying amounts of magnesium oxide if dolomitic limestone is used, calcium sulfate depending on the sulfur content of the kiln fuel, fly ash when coal is used as the fuel, and dust from limestone handling and unburned limestone. Other impurities such as silica, iron, aluminum, and other metals may also be present, but in very small amounts, because the limestone used for the manufacture of lime is typically quite pure to meet chemical standards. LKD differs from commercial lime in that the raw ingredients in LKD have not been fully burned.|[0037] LKD has a specific gravity that typically falls between 2.4 and 3.0 and a bulk density that falls between 720-1150 kg/m3. The particle size range of LKD falls between 0.005 mm and 2.0 mm and generally 75% of the material passes through a 0.03 mm (No. 450 sieve). The amount of calcium oxide and amount of free-lime present in LKD varies between lime manufacturing facilities depending on the source of the limestone and kiln process used.|[0038] Slag cement (also called ground granulated blast furnace slag) is a hydraulic cement produced during the reduction of iron ore to iron in a blast furnace. Molten slag is tapped from a blast furnace, rapidly quenched with water (“granulated”), dried, and ground to a fine powder. The rapid quenching ‘freezes’ the molten slag in a glassy state, which gives the product its cementitious properties.|[0039] When iron is manufactured using a blast furnace, the furnace is continuously charged from the top with oxides, fluxing material, and fuel. Two products—slag and iron—collect in the bottom of the hearth. Molten slag floats on top of the molten iron; both are tapped separately. The molten iron is sent to the steel producing facility, while the molten slag is diverted to a granulator. This process, known as granulation, is the rapid quenching with water of the molten slag into a raw material called granules. Rapid cooling prohibits the formation of crystals and forms glassy, non-metallic, silicates and alumino-silicates of calcium. These granules are dried and then ground to a suitable fineness, the result of which is the slag cement. The granules can also be incorporated as an ingredient in the manufacture of blended portland cement. Slag cement (ground granulated blast furnace slag) typically has a specific gravity that falls between 2.85 and 2.94, and consists of about 45% CaO, 33% SiO2, 10% Al2O3, 1% Fe2O3, and 6% MgO.|[0040] In a next process step of FIG. 1, cement-kiln dust, lime kiln dust, and/or slag cement are combined with foam from the foam generator and water in a mixer (wet unloader) to form a foamed mixture. Various foamed mixtures of the cementitious material, foam and water are possible. In one specific embodiment, the foamed mixture includes about 1275 pounds of cement-kiln dust per cubic yard of the foamed mixture and about 960 pounds of water per cubic yard of the foamed mixture. In another specific embodiment, the foamed mixture includes about 1575 pounds of lime-kiln dust per cubic yard of the foamed mixture and about 660 pounds of water per cubic yard of the foamed mixture. In a third specific embodiment, the foamed mixture includes about 1600 pounds of slag cement per cubic yard of the foamed mixture and about 650 pounds of water per cubic yard of the foamed mixture. These specific embodiments are not limiting in the possible proportions of cementitious material, water, and foam that could be used in the foamed mixture. Also, an over dosage of foam is beneficial in certain cases because of the instability/breakdown of the foam during mixing.|[0041] In addition to cement-kiln dust, lime kiln dust, or slag cement, other cementitious materials may also be used in the foamed mixture. Examples of other cementitious materials that could be added include portland cement and fly ash. It is also contemplated that other materials, such as fine aggregate and coarse aggregate, may be included in the foamed mixture. However, in certain embodiments, the foamed mixture may consist essentially of water, cement-kiln dust and foam; water, lime-kiln dust and foam; or water, slag cement and foam. This avoids the need to integrate other materials into the foamed mixture that may affect properties of the final cured product.|[0042] After the foamed mixture is prepared, different process steps may be undertaken. In Option #1 of FIG. 1, the foamed mixture is removed from the mixer and loaded onto a vehicle that transports the foamed mixture to a curing station where the foamed mixture sets. In geographic locations where cold winters are experienced, the foamed mixture may be transported to a curing station in the power plant building or to a below ground silo/bin. In order to accelerate curing/setting of the foamed mixture, flue gas and/or low grade stream heat, preferably recovered from the power plant, are passed over and/or through the foamed mixture. During the summer season, or in geographic locations where cold winters are not experienced, the foamed mixture may be transported to an outdoor storage pile for curing/setting of the foamed mixture.|[0043] During curing/setting of the foamed mixture, the carbon dioxide in the flue gas dispersed in the foaming agent reacts with hydration products in the foamed mixture and in turn sequesters the carbon dioxide. The cured/set foamed mixture typically meets the standards for controlled low-strength materials as published by the American Concrete Institute. For example, the process of the invention produces a controlled low-strength material that results in a compressive strength of 8.3 MPa (1200 psi) or less at the conventional 28 day testing period, and may produce a controlled low-strength material with unconfined compressive strengths of 2.1 MPa (300 psi) or less at the conventional 28 day testing period.|[0044] Referring still to FIG. 1, after curing/setting of the foamed mixture, the cured mass may be crushed into aggregate and thereafter screened into an undersize fine aggregate fraction and a coarse aggregate fraction that meets a predetermined coarse aggregate material specification such as those published by the American Society for Testing and Materials.|[0045] In Option #2 of FIG. 1, the foamed mixture is removed from the mixer and fed to a shaping device such as a pan pelletizer, extruder or briquetter for shaping into aggregate. In geographic locations where cold winters are experienced, the shaped aggregate is conveyed to a curing station in the power plant building or to a below ground silo/bin. In order to accelerate curing/setting of the shaped aggregate, flue gas and/or low grade stream heat, preferably recovered from the power plant, are passed over and/or through the shaped aggregate. During the summer season, or in geographic locations where cold winters are not experienced, the shaped aggregate may be transported to an outdoor storage pile for curing/setting of the shaped aggregate.|(US9028607)|EXAMPLES|[0046] The following Examples have been presented in order to further illustrate the invention and are not intended to limit the invention in any way.|1. Experimental Overview|[0047] The experiments detailed below included performance testing and evaluation of foamed controlled low-strength materials (CLSM) produced using a commercial foam generator. The CLSM included mixtures of cement-kiln dust, water, and foam; lime-kiln dust, water, and foam; and slag cement, water, and foam. The CLSM were produced using the foam generator with one of three different types of compressed gases: air, carbon dioxide, and a mixed gas. This mixed gas was used to simulate a typical flue gas generated from the combustion of coal at a typical electric power plant. The experiments explored the feasibility of using flue gas to generate a low-density CLSM with sufficient strength to be used as a lightweight aggregate. It was determined that the use of the flue gas promotes carbonation of the sample thereby increasing the compressive strength and binding the carbon dioxide in the carbonation reaction. It was also determined that the carbonation reaction of the CLSM could reduce carbon dioxide emissions at a coal-fired power plant. The use of a foam generator was intended to have two effects on the CLSM produced, to lower the density of the material, and to distribute the selected gas throughout the CLSM. The distributed gas bubbles would then provide a source for the carbonation reaction within the CLSM.|2. Materials|A. Cementitious Materials|Cement-Kiln Dust, Lime-Kiln Dust, and Slag Cement|[0048] Cement-kiln dust was obtained from the Lafarge North America cement manufacturing facility located in Alpena, Mich. Dolomitic lime-kiln dust was obtained from the Western Lime manufacturing facility located in Eden, Wis. Slag cement was obtained from the Holcim (U.S.) Inc. facility located in Chicago, Ill.|[0049] Moisture contents of the three cementitious by-product materials collected for use in these examples were obtained by thermo gravimetric analysis in accordance with ASTM C 311, “Standard Test Method for Sampling and Testing of Fly Ash or Natural Pozzolans for use in Portland Cement Concrete.” The moisture content test results are shown in Table 1.|[0050] TABLE 1 Percent Moisture   Percent   Initial Mass(%)Average Material(gm)Moisture% Moisture   CKD1.0460.067  CKD1.158−0.0860.021 CKD1.2480.120 LKD1.8380.266 LKD1.4180.2260.23 LKD1.5510.200 Slag1.5120.106 Slag1.6200.0740.09 Slag1.5210.079  |[0051] Loss-on-ignition (LOI) values for the three cementitious by-product materials collected for use in these examples were obtained by thermo gravimetric analysis in accordance with ASTM C 311, “Standard Test Method for Sampling and Testing of Fly Ash or Natural Pozzolans for use in Portland Cement Concrete.” The measured values for loss on ignition represent the consumption of organic material such as carbon and the volatilization of the alkali compounds found in the materials. The CKD and LKD are not fully calcined and the higher numbers shown represent completion of this process combined with combustion of any residual organic compounds such as carbon. The slag is produced at very high temperatures and is calcined with very few organics present to be removed in this test. In the case of slag, the material is actually absorbing a small amount of mass from the test atmosphere elements present. The LOI results are shown in Table 2.|[0052] TABLE 2 Percent Loss on Ignition (LOI) - Dry Basis  Initial MassPercent (%)PercentAverage Material(gm)Ash(%) LOI% LOI   CKD1.04690.679.268  CKD1.15890.379.7119.4 CKD1.24890.629.276 LKD1.83877.2722.53 LKD1.41877.3422.4922.5 LKD1.55177.4422.41 Slag1.512100.5−0.583 Slag1.620100.5−0.562−0.6 Slag1.521100.5−0.586  |[0053] The density and specific gravity of each material was obtained by standard gravimetric analysis in accordance with ASTM C 188, “Standard Test Method for Density of Hydraulic Cement” and ASTM C 311, “Standard Test Method for Sampling and Testing Fly Ash or Natural Pozzolans for Use in Portland-Cement Concrete.” The values measured were in the expected ranges for these by-product materials, and are shown in Table 3.|[0054] TABLE 3 Specific Gravity of Materials  Actual MassVolumeSpecificAverage Material(gm)(ml)GravitySG   CKD67.4123.22.911  CKD64.0621.42.9992.98 CKD63.9921.23.024 LKD63.5422.62.817 LKD60.6421.62.8132.80 LKD62.2222.52.771 Slag51.0717.72.891 Slag55.6918.33.0492.97 Slag55.7118.82.969  |[0055] The three finely divided mineral by-products were analyzed for oxides content by the X-ray fluorescence test method (ASTM D 4326, “Standard Test Method for Major and Minor Elements in Coal and Coke Ash by X-ray Fluorescence”). All three by-products had substantial amounts of compounds with the potential capability to react with CO2 and form carbonate minerals. The calcium oxide (lime) content was found to be highest in the cement kiln dust at 49.8% followed by the blast furnace slag at 38.2%, and lime kiln dust at 32.7%. The magnesium oxide content was found to be the highest in the dolomitic based lime kiln dust at 24.9%, followed by blast furnace slag at 11.0%, and cement kiln dust at 2.2%. Complete results are shown in Table 4.|[0056] TABLE 4 Mineral Oxides Analysis of By-Product Materials (%)  CementLimeBlast  KilnKilnFurnace MineralDustDustSlag Analysis(CKD)(LKD)(SLG)   SiO214.479.539.2 Al2O35.14.810.4 Fe2O32.01.10.7 CaO49.832.738.2 MgO2.224.911.0 K2O3.80.80.4 SO312.30.51.2 TiO20.00.00.4 LOI 750° C.9.422.5−0.5 LOI 1000° C.10.524.9−1.5 SUM100.0100.0100.0 Available6.84.00.5 Alkali  |B. Foam Concentrate|[0057] A foam concentrate solution was used for generating foam. The foam concentrate was obtained from Elastizell Corporation of America, Dexter, Mich., USA. Prior to mixing the CLSM, the foam concentrate was diluted with water at a ratio of 40 parts of water to one part of foam concentrate by volume. Temperature of the water used to mix the foam concentrate was increased when carbon dioxide was used to generate the foam.|C. Compressed Gas|[0058] Three types of compressed gas were used to generate the foam: compressed air, carbon dioxide, and a gas used to simulate flue gas from a coal burning electric power plant. Dry air at sea level typically contains, among other things, 75.53 wt. % nitrogen, 23.16 wt. % oxygen and 0.033 wt. % carbon dioxide. The simulated flue gas consisted of a mixture of carbon dioxide, sulfur dioxide, nitrogen, and nitrous oxide. The carbon dioxide concentration in the simulated flue gas was 11.7%.|D. Foam Generator|[0059] The foam generator was a Mini (½″) Open Air-Foam-Generating System (MiniOAS) manufactured by Elastizell that included a regulator, diaphragm pump, and foam mixing nozzle. Two pressure regulators were used for the compressed gas supply, one at the compressed gas tank, and the second at the foam generator. Gas from the tank was regulated to a pressure of 175 psi prior to introduction in the foam generator. When using carbon dioxide, a rubber hose extension, approximately six feet long, was used to warm the carbon dioxide gas before introduction into the foam generator. Without the additional length of hose, the foam generator began to freeze and leak gas.|[0060] The regulator on the foam generator was adjusted to 100 psi. The intake hose from the diaphragm pump was placed in the foam concentrate solution which was diluted using the ratio specified by the manufacturer of 40 parts of water to one part of foam concentrate by volume. The valve on the foam nozzle was opened and foam was generated until it reached a uniform quality (within approximately 5 to 10 seconds). The valve on the nozzle was then closed until foam was to be added to the CLSM mixture.|[0061] Foam density tests were performed for each of the three compressed gases used in foam production. The foam generator was started and flushed with clear water and then switched over to the 1 to 40 foaming agent to water mixture. The foam generator was re-started, and once a consistent stream was being produced, the foam was directed to fill a series of five-gallon pails. Each five-gallon pail was weighed and divided by its measured volume to arrive at the foam density values shown in Table 5. The stability of the foam produced with air and flue gas was excellent; however, the foam produced with the CO2 decreased in volume linearly with time as shown in Table 6.|[0062] TABLE 5 Foam Density   Avg. Wt.   Weight (lb)(lb) Foam Temp.(per(perDensityGas Type(Degrees F.)5-gal Pail)5 gal Pail)(lb/cu ft)  601.76  Air (First Run)601.761.772.65 601.78 651.82Air (Second Run)651.881.782.66 651.64 452.20Flue Gas (First Run)452.302.223.24 452.16 482.36Flue Gas (Second482.442.473.70Run) 482.60 602.93CO2 (First Run)603.023.024.52 603.12 1002.52CO2 (Second Run)1002.822.794.17 953.04 902.76CO2 (First Run)902.822.874.29w/Heater) 923.04 952.96CO2 (First Run)952.622.774.14w/Heater) 952.74 |[0063] TABLE 6 CO2 Foam Loss versus Time Foam Height  Time (minutes)(in)Foam Loss (in)Loss (in/min) 014.75——113.50−1.251.25212.25−2.501.25311.00−3.751.25410.25−4.500.7558.75−6.001.50Average  1.20 |[0064] It was believed that the foam loss for the CO2 foam may be related to the cold temperature associated with the expanding compressed CO2 gas. Two measures were employed to produce a stable-foam. Warm water was used with the foam concentrate and a heater-line was wrapped to help warm the CO2 gas while being transported from the compressed air tank to the foam generator. The temperature of foam produced ranged from 60° F. (16° C.) up to 100° F. (38° C.). These improvements were successful in producing a stable-foam.|3. Manufacturing of CLSM Mixtures|[0065] CLSM was mixed using a two-cubic foot (0.057 m3) capacity tilting drum Gilson concrete rotating-drum mixer. All CLSM ingredients were manually weighed and loaded in the mixer. The required amounts of the cement-kiln dust, lime-kiln dust, or slag cement and water were loaded into the mixer and mixed for three minutes. If during the mixing process, the cementitious material agglomerated and adhered to the inside surface of the mixer, the mixer was briefly stopped, material was scraped from the mixer surface and then restarted for the remaining time. The desired volume of the foam was then added to the CLSM with the mixer running. The amount of foam was specified as a volume for each mixture. When the foam had uniformly mixed into the CLSM, the CLSM was discharged into a container of known volume for tests of unit weight, density and temperature. Each final mixture was them poured into a minimum of twenty four 4 in. x 8 in. cylinder molds (pre-split for easy sample removal and for reuse) for casting of test specimens.|4. CLSM Specimen Preparation and Testing|[0066] 4-inch diameter by 8-inch long cylindrical test specimens were prepared from each final mixture for compressive strength (ASTM D 4832) and carbonation testing (RILEM CPC18). Compressive strengths of the final CLSM mixtures were evaluated at the specified ages of 7, 14, 28, 56, 91, and 182 days. All test specimens were cast in accordance with ASTM D 4832. Three CLSM test specimens were tested at each test age for each of the nine test mixture materials (three by-products and three types of gases), and an average compressive strength was obtained for each test mixture.|[0067] All of the test specimens were allowed to cure in molds together for three days indoors in the laboratory where they were made. The plastic cylinder molds were then removed from the test specimens and they were moved to a curing chamber and subjected to roughly a 0.03% CO2 concentration found in the ambient air, with the lab temperature of 20° C.+/−2° C. (70° F.+/−3° F.), and relative humidity of 65%+/−25%. A humidifier was used to add moisture to the curing chamber air during storage when the indoor air was dry in the room where the curing chamber was located. The cylinders were spaced at least 0.8 in (20 mm) apart in the curing chamber so that air was able to reach the test surfaces unhindered at all times and continued carbonation could take place. The specimens were kept in the curing chamber until needed for strength and carbonation testing.|5. Carbonation Evaluation|Depth of Carbonation and Percent by Mass CO2 |[0068] In order to evaluate the effects of the different mixtures used in the foamed CLSM, carbonation of the mixtures was first tested in accordance with RILEM test procedure CPC18, Measurement of Hardened Concrete Carbonation Depth (Materials and Structures, Vol. 21, No. 126, November-December 1988). In accordance with this test procedure, a phenolphthalein indicator solution is sprayed onto a broken section of test cylinder. A solution of 1% phenolphthalein in 70% ethyl alcohol was used. The cylinders used for the carbonation measurement were first tested for splitting-tensile strength. The broken surface of the cylinder was lightly brushed (with a horse-hair brush to avoid damaging the surface of the CLSM) to remove loose particles, and then sprayed with the indicator solution. Typically, the indicator solution was applied approximately two to three minutes after completion of the test for splitting-tensile strength. Carbonated areas of the test specimens remain colorless, while non-carbonated areas turn pinkish-red. Measurements for the depth of carbonation were taken after one to two minutes of application of the indicator solution.|[0069] A percent CO2 by mass test was then performed on the samples. In contrast to the phenolphthalein indicator tests intended to record the depth of carbonation at points in time, the percent CO2 by mass tests are intended to record the mass percentage of CO2 embodied within the full-depth of the carbonated zone as indicated by the phenolphthalein indicator test at these same points in time. A portion of the carbonated cylinder (as determined from the phenolphthalein indicator test), from each type of mortar material, was sealed in a plastic food-grade bag for testing per ASTM C 25, “Standard Test Method for Chemical Analysis of Limestone, Quicklime, and Hydrated Lime,” for carbon dioxide content. Immediately after compression testing and carbonation testing, samples were vacuum-sealed in the plastic bags. At the time of testing for CO2 percent by mass, the carbonated portion of the samples were removed from the vacuum sealed bags. The samples were filed to the full depth of carbonation, and the filings were collected for further preparation by grinding in a mortar and pestle.|[0070] The ASTM C 25 gravimetric test method was used for quantifying the amount of carbon dioxide contained within each sample. The samples were decomposed with hydrochloric acid and the liberated CO2 was passed through a series of scrubbers to remove water and sulfides. The CO2 was absorbed with Ascarite, a special sodium hydroxide absorbent, and the gain in weight of the absorption tube was determined and calculated as percent CO2.|6. Mixture Proportions|A. CLSM Trial Mixture Proportions|[0071] A small batch in a 0.15 ft3 (4248 cm3) mixing bowl was produced for each of the three by-product materials with compressed-air generated foam to obtain an indication of behavior with the foaming agent and the need for a retarding admixture in case of rapid setting. Each material was unique in its behavior with foam and affinity for water. Air content of the mixture was targeted at 30% for all these mixtures. Table 7 shows the actual proportions used for the small-scale trial batch mixtures.|[0072] TABLE 7 Actual Mixture Proportions for Small-Scale Trail Batch Mixtures MixtureBy-Product   (Material -MaterialWaterAir Content Gas)(lb/yd3)(lb/yd3)(%)   CKD - A143211006.2 LKD - A149862631.1 SLG - A133154840.9  |[0073] The resulting densities and percent air contents for each mixture are shown in Table 8. These results were used to determine final mixture proportions for each of the by-product materials, as each by-product material had different water demands and behaved differently with the foaming agent. The targeted dry density needed to fall in the range of 60 to 90 pounds per cubic foot (962 to 1443 kg/m3) to provide lower density properties when compared to normal aggregates with densities over 100 pounds per cubic foot (1604 kg/m3).|[0074] TABLE 8 Density of Small-Scale Mixtures   Percent Air  Air Dry Density(Wet), Wet Density (lb/ft3),(lb/ft3)immediatelyMaterialimmediately after mixing(after 28 days)after mixing CKD94.788.36.2LKD79.473.631.1Slag72.765.140.9 |B. CLSM Final Mixtures Proportions|[0075] CLSM final mixture proportions and fresh properties for the foamed-CLSM mixtures are given in Table 9, which shows the amount of ingredients used for each 1.8 cu ft (0.051 cu m) batch of foamed mortar produced. The wet cylinder weight was targeted at 4.8 pounds+/− one pound (2.2 kg+/−0.45 kg) for consistency of density. Additional quantities of carbon dioxide based foam were required to obtain the desired range of density due to the instability of the foam after formation. This can be readily identified on Table 9 when the amounts of foam used in mixtures with CO2 (CKD+CO2, etc.) are compared to the amounts of foam used for the compressed air and flue gas based foam mixtures (CKD+Air and CKD+Flue Gas, etc.) for each by-product set of mixtures.|[0076] TABLE 9 Mixture Proportions and Fresh Mortar Data for 1.8 ft3 Batches CKD +CKD +CKD +LKD +LKD +LKD +Slag +Slag +Slag + AirFlue GasCO2AirFlue GasCO2AirFlue GasCO2  By-product858583.2105105105107107107(lb)Foam342564156.5715(gallon)Water646464444444434343(lb)Retarder000000000(ml)Class C000000000Fly Ash(lb)Flow101114911.5197.5714(in)Temperature34373220132010910Rise (° F.)Wet4.84.75.24.05.05.74.94.94.9Cylinder Weight (lb) |7. Mechanical Properties|A. CLSM Compressive Strength|[0077] CLSM has a maximum compressive strength specified by ACI Committee 229 as 1,200 psi at the age of 28 days. A desirable compressive strength level of CLSM at the 28-day age, for applications where the CLSM is used as a fill material and required to be removed at a later age, by the use of hand shovels, is usually specified to be less than 100 psi.|[0078] The by-product-based materials tested are low-strength compared to concrete and fall in the range of CLSM, with a required compressive strength of 1200 psi (8.3 MPa) or less. Table 10 provides the compressive strength test data obtained for the cement-kiln dust mixtures. All three of the CKD mixtures attained strength of at least 200 psi (1.38 MPa) by the 56-day age. At the conclusion of testing at the 182-day age the strength varied to a range of 209 to 217 psi (1.44 to 1.50 MPa) at the 182-day age.|[0079] TABLE 10 Average Compressive Strength Test Results for the CKD Mixtures MIXTURE AgeCKD + AirCKD + Flue GasCKD + CO2 (Days)(psi)(psi)(psi)   7495537 14167123128 28234178241 56207232279 91297240282 182216209217  |[0080] Table 11 provides the compressive strength test data obtained for the lime-kiln dust mixtures. The LKD mixtures produced with compressed CO2 gas provided the highest strength of 623 psi (4.30 MPa) at the 56-day age, followed by the flue gas mixture with a strength of 182 psi (1.26 MPa) and the compressed air mixture was lowest with 84 psi (0.59 MPa). The same strength pattern occurred at the later ages with no significant strength gain.|[0081] TABLE 11 Average Compressive Strength Test Results for the LKD Mixtures MIXTURE AgeLKD + AirLKD + Flue GasLKD + CO2 (Days)(psi)(psi)(psi)   7243364 1473125197 28123190294 5684182623 91130265366 18254163591  |[0082] Table 12 provides the compressive strength test data for the slag mixtures. The slag mixture produced with compressed flue gas provided the highest strength at the 56-day age of 206 psi (1.42 MPa), followed by the CO2 gas mixture with a strength of 193 psi (1.33 MPa), and the compressed air mixture was lowest at 91 psi (0.63 MPa) at the 56-day age. At the 91-day test age the slag based mixture produced with compressed CO2 had the highest strength of 253 psi (1.74 MPa) followed by the flue gas mixture with 206 psi (1.42 MPa), and finally the compressed air mixture with 162 psi (1.12 MPa). At the 182-day age the compressed air mixture provided the highest compressive strength at 173 psi (1.19 MPa) followed by the CO2 mixture with a compressive strength of 169 psi (1.17 MPa) and the flue gas mixture provided a strength of 131 psi (0.90 MPa).|[0083] TABLE 12 Average Compressive Strength Test Results for the Slag Mixtures MIXTURE AgeSlag + AirSlag + Flue GasSlag + CO2 (Days)(psi)(psi)(psi)   7105181109 14141182130 28100212238 5691206193 91162206253 182173131169  |[0084] A review of the compressive strength results for the mixtures produced with compressed air shows that the CKD mixture clearly concluded the tests with the highest compressive strength of 216 psi (1.49 MPa) followed by the slag mixture at 173 psi (1.19 MPa). The compressive strength of the LKD by-product material was below 54 psi (0.52 MPa), well below the strengths of the CKD and slag mixtures.|[0085] A review of the compressive strength results for the mixtures produced with the compressed flue gas shows that the CKD, LKD and slag mixtures concluded in relative proximity to each other at 209 psi (1.44 MPa), 163 psi (1.12 MPa) and 131 psi (0.90 MPa) respectively.|[0086] A review of the compressive strength test results for the mixtures produced with the compressed CO2 gas shows that the LKD mixture clearly concluded the tests with the highest compressive strength of 591 psi (4.08 MPa). The CKD and slag mixtures concluded in relative proximity to each other at 217 psi (1.50 MPa) and 169 psi (1.17 MPa) respectively.|[0087] In summary, the compressive strengths were all comparable for the three CKD materials produced at all ages tested. The compressive strength of LKD was highest for the compressed CO2 mixture followed by flue gas and then the air mixture. The compressive strengths of the three slag materials produced were comparable at all ages.|8. Carbonation Testing|A. Depth of Carbonation of CLSM Mixtures|[0088] The carbonated depth measurements at different ages for the cement-kiln dust mixtures are given in Table 13. The test results for carbonation depth measurements on the CKD materials show an expected near-linear increase with respect to time. The CKD materials foamed with air and flue gas carbonated at nearly the same rate from an age of one week to six months. The CKD material foamed with CO2 also shows a linear increase in carbonation depth with no carbonation recorded at the seven day age and concluding at a measured carbonation depth of 0.875 in (22 mm) at the six month age. This compares to a depth of one inch (25 mm) for the materials foamed with air and flue gas at the six month age. This small difference may relate to the CO2 based foam stability in the fresh mixtures, and possible variability in permeability providing a more difficult pathway for interaction with the curing atmosphere in the CO2 based foam.|[0089] If the hardened foamed material were crushed into a ¾ inch (19 mm) aggregate at an early age, and if carbonation occurred inward from outside edges at a similar rate to these cylinders, the aggregate would achieve full-carbonation within 56 days of storage for all three types of the gases used. Similarly, full-carbonation of a one inch (25 mm) nominal size aggregate could be accomplished in 91 days.|[0090] TABLE 13 Carbonation Depth for Hardened CKD Materials CKD (Days)Air (in)Flue Gas (in)CO2 (in)   70.031250.062500 140.125000.125000.12500 280.250000.250000.12500 560.406250.437500.37500 910.625000.625000.50000 1821.000001.000000.87500  |[0091] The carbonation depth at different ages of the lime-kiln dust mixtures are shown on Table 14 with the various CO2 containing gases used in production. The test results for carbonation depth measurements on the LKD materials indicate a slow start of carbonation through the seven day age and then the expected near-linear increase in carbonation depth with respect to time. The LKD material foamed with air carbonated to the greatest depth after six months at 1.25 in (32 mm) followed by the material foamed with flue gas with a carbonation depth of 0.75 in (19 mm) and then the material foamed with CO2 with a depth of 0.625 in (16 mm). The LKD material foamed with air was carbonated to a depth 67% greater than the material foamed with flue gas and 100% greater than the material foamed with CO2 gas at the six month age. The carbonation differences may be related to permeability differences between the three samples foamed with the different gases. The foaming agent used in these tests is designed for use with compressed air. The introduction of flue gas and CO2 gas may influence the size and spacing of air bubbles in the carbonated material, possibly affecting the materials' permeability and the ability of the curing atmosphere to reach the carbonation sites.|[0092] If the hardened foamed material were crushed into a ¾ inch (19 mm) aggregate at an early age, and carbonation occurred inward from outside edges similar to the cylinders tested, the aggregate would achieve carbonation within 56 days of storage for all three gases used. Similarly, carbonation of a one inch (25 mm) nominal size aggregate could be accomplished in 91 days.|[0093] TABLE 14 Carbonation Depth for Hardened LKD Materials LKD (Days)Air (in)Flue Gas (in)CO2 (in)   70.000000.000000.00000 140.218750.125000.06250 280.312500.562500.18750 560.500000.500000.37500 910.937500.500000.62500 1821.250000.750000.62500  |[0094] The carbonation depth at different ages of the slag mixtures produced are shown on Table 15 with the various CO2 containing gases used in production. The measurements for carbonation depth on the slag materials indicate an expected near-linear increase with respect to time. The phenolphthalein indicator test indicated that at the seven day age, no carbonation had occurred with slag materials foamed with CO2, but the slag material foamed with air showed a carbonation depth of 0.03125 in (0.8 mm) and the material foamed with flue gas showed a depth of 0.0625 in (1.6 mm). At 14 days, all three slag based materials had a carbonation depth of 0.125 in (3.2 mm). At 28 days, the slag based materials foamed with air and flue gas each measured a depth of 0.25 in (6.4 mm), and the slag material foamed with CO2 showed a carbonation depth of 0.125 in (3.2 mm). At 56 days the carbonation depth of slag material foamed with flue gas measured 0.4375 in (11 mm) followed by the slag material foamed with air at 0.40625 in (10 mm) and 0.375 in for the material foamed with CO2. At 91 days, the slag material foamed with air showed a carbonation depth of 1.0 in (25 mm), the material foamed with flue gas showed a carbonation depth of 0.625 in (16 mm). The material foamed with CO2 measured 0.50 in (13 mm) at both the 91 day and six month ages. At the six month age, the slag material foamed with air showed a carbonation depth of 1.25 in (32 mm) and the material foamed with flue gas showed a carbonation depth of 1.50 in (38 mm). The carbonation differences may be related to permeability variations between the three samples foamed with the different gases.|[0095] If the hardened foamed material were crushed into a ¾ inch (19 mm) aggregate at an early age, and carbonation occurred inward from outside edges similar to the cylinders tested, the aggregate would achieve carbonation within 56 days of storage for all three gases used. Similarly, carbonation of up to a two inch (51 mm) nominal size aggregate could be accomplished with compressed air and up to a one inch (25 mm) nominal size aggregate could be accomplished with flue gas and CO2 gases in 91 days.|[0096] TABLE 15 Carbonation Depth for Hardened Slag Materials Slag    (Days)Air (in)Flue Gas (in)CO2 (in)   70.125000.062500.12500 140.250000.250000.12500 280.562500.250000.18750 560.750000.406250.37500 911.000000.625000.50000 1821.250001.500000.50000  |[0097] A review of the data shows that all of the compressed gases used (air, flue gas, or carbon dioxide) in the production of the foam based CLSM had similar effects on the rate of carbonation for each of the specific by-product-based materials tested. It appear that the chemical make-up of the by-product-based materials had a greater influence on the rate of carbonation than the concentration of CO2 in the various compressed gases used.|B. CO2 Percent by Mass of CLSM Mixtures|[0098] Table 16 provides the results of ASTM C 25, “Standard Test Method for Chemical Analysis of Limestone, Quicklime, and Hydrated Lime,” gravimetric testing method for CO2 by mass for the cement-kiln dust based materials. The CO2 content determined for CKD at an age of zero days represents the mass percentage of CO2 in a sample of the raw material, before it was used in production of the foamed CLSM. The CKD was provided by Lafarge North America from the cement manufacturing facility located in Alpena, Mich. All other values given in Table 16 are from the carbonated portion of the cured cylinders and are the values obtained from ASTM C 25 testing of the CKD based materials formed with the gases shown. The CKD powder originally contained 9.5% CO2 by mass. This amount increased after 182 days to 20.7%, 21.0% and 19.2% for the CKD based materials foamed with compressed air, flue gas and CO2 respectively.|[0099] TABLE 16 Percent CO2 by Mass of CKD-Based Carbonated Materials Time Flue Gas  (Days)Air (% CO2)(% CO2)CO2 (% CO2)   09.5—— 721.818.17.0 1418.317.216.7 2819.118.819.4 5619.921.018.9 9120.220.218.2 18220.721.019.2  |[0100] Table 17 provides the results of the ASTM C 25, “Standard Test Method for Chemical Analysis of Limestone, Quicklime, and Hydrated Lime,” gravimetric testing method used for the determination of CO2 by mass from the lime-kiln dust based materials. The CO2 content determined for LKD at an age of zero days represents the mass percentage of CO2 in a sample of the raw material before it was used in production of the foamed CLSM. The LKD was provided by Western Lime Corporation from the lime manufacturing facility located in Eden, Wis. All other values given in Table 17 are from the carbonated portion of the cured cylinders, and are the values obtained from ASTM C 25 testing of the LKD based materials formed with the gases shown. The original LKD powder contained 22.2% CO2 by mass. This amount increased after 182 days to 25.9%, 25.7% and 25.6% of the mass for the LKD-based materials foamed with compressed air, flue gas, and CO2 respectively.|[0101] TABLE 17 Percent by Mass CO2 of LKD-Based Carbonated MaterialsTime   (Days)Air (% CO2)Flue Gas (% CO2)CO2 (% CO2) 022.2——720.721.820.91423.323.724.72824.022.724.65624.825.024.69125.025.324.818225.925.725.6 |[0102] Table 18 provides the results of the ASTM C 25, “Standard Test Method for Chemical Analysis of Limestone, Quicklime, and Hydrated Lime,” gravimetric testing method used for the determination of CO2 by mass from the slag based materials. The CO2 content determined for the slag at an age of zero days represents the mass-percentage of CO2 in a sample of the raw material before it was used in production of the foamed CLSM. The slag was provided by Holcim (US) Inc. from the slag manufacturing facility located in Chicago, Ill. All other values given in Table 18 are from the carbonated portion of the cured cylinders, and are the values obtained from ASTM C 25 testing of the slag based materials formed with the gases shown. The original slag contained 1.4% CO2 by mass. This amount increased after 182 days to 5.2%, 5.1% and 4.7% of the mass for the slag-based materials foamed with compressed air, flue gas and CO2 respectively.|[0103] TABLE 18 Percent by Mass CO2 of Slag-Based Carbonated Materials Time Flue Gas  (Days)Air (% CO2)(% CO2)CO2 (% CO2)   01.4—— 72.57.21.8 145.14.04.1 283.24.55.2 563.84.55.3 917.35.05.2 1825.25.14.7  |[0104] For the three by-product-based materials made with compressed air, there was a net increase in the measured CO2 content by percent mass in each case. The CO2 content of the CKD-based materials more than doubled from a starting value of 9.5% to 20.7% after six months and the percent CO2 content by mass times volume also increased. The CO2 content of the LKD-based materials increased modestly from a starting value of 22.2% to 25.9% after six months and the percent CO2 content by mass times volume also increased. The slag-based material had a starting value of 1.4% and increased by nearly four times to 5.2% after six months, and the percent CO2 content by mass times volume also increased.|[0105] For the three by-product-based materials made using compressed flue gas, there was also a net increase in the measured CO2 content over time in each case. The CO2 content of the CKD-based materials more than doubled from a starting value of 9.5% to 21.0% after six months, and the percent CO2 content by mass times volume also increased. The CO2 content of the LKD-based materials increased modestly from a starting value of 22.2% to 25.7% after six months, and the percent CO2 content by mass times volume also increased. The slag had a starting value of 1.4% and increased by over three times to 5.1% after six months, and the percent CO2 content by mass times volume also increased.|[0106] Finally, the three by-product-based materials made using compressed carbon dioxide gas also showed a net increase in the measured value of CO2 in each case. The CO2 content of the CKD-based materials nearly doubled from a starting value of 9.5% to 19.2% after six months, and the percent CO2 content by mass times volume also increased. The measured value of CO2 content of the LKD-based materials increased modestly from a starting value of 22.2% to 25.6% after six months, and the percent CO2 content by mass times volume also increased. The slag-based material had a measured CO2 starting value of 1.4% and increased to 4.7% after six months, and the percent CO2 content by mass times volume also increased.|[0107] These results illustrate that for all of the CO2 containing compressed gases used, the by-product materials have significant CO2 sequestration properties. For all of the CO2 containing gases used, the total amount of CO2 sequestered was highest in the LKD aggregates, followed by the CKD and Slag aggregates.|9. Measured Properties for Foamed-CLSM Aggregates|[0108] For the purposes of illustration only, Tables 19-20 provide properties for the materials prepared above from cement-kiln dust, lime-kiln dust, and slag cement in relation to American Society for Testing and Materials (ASTM) specifications and properties of other materials. Each of the nine materials created above (three different by-products each combined with three different gases) were crushed into aggregates. The crushed aggregate materials were tested for characteristics that would allow for comparison to other materials.|[0109] Table 19 shows test results for the measurement of five different physical properties for the crushed aggregates made from the by-product based CLSM: bulk density in a dry-rodded state (density), absorption, specific gravity, fineness modulus, and staining test results.|[0110] The bulk density in a dry-rodded state is defined in ASTM C 29, “Standard Test Method for Bulk Density (Unit Weight) and Voids in Concrete,” as “the mass of a unit volume of bulk aggregate material, in which the volume includes the volume of the individual particles and the volume of the voids between the particles.” The bulk density relationship is important for planning packaging and transportation commercial arrangements. The density compared to other materials is also helpful in planning geotechnical and concrete product applications. The dry-rodded bulk densities for the by-product-based aggregates fall in the range of 44.2 to 61.8 lb/ft3.|[0111] Absorption is defined in ASTM C 127, “Standard Test Method for Density, Relative Density (Specific Gravity), and Absorption of Coarse Aggregate,” as “the increase in mass of aggregate due to water penetration into the pores of the particles during a prescribed period of time, but not including water adhering to the outside surface of the particles, expressed as a percentage of dry mass.” The aggregates were soaked in water for 24 hours (plus or minus 4 hours) and then dried in towels to the saturated surface dry (SSD) condition. The absorption values ranged from a low value of 18.1 percent for the slag foamed with CO2 aggregate material to a high of 48.7 for the CKD foamed with CO2 aggregate material. The absorption property is important in calculating the change in density from a dry to SSD condition for storage, packaging and transportation purposes. Absorption is also an important property for performing water content calculations in concrete mixture proportioning, and in calculating internal curing potential for lightweight aggregate concrete.|[0112] Specific gravity is defined in ASTM C 127, “Standard Test Method for Density, Relative Density (Specific Gravity), and Absorption of Coarse Aggregate,” as “the ratio of the density of the aggregate (oven dry) to the density of distilled water at a stated temperature” which in this case was 73° F. (23° C.). Specific gravity is commonly used for volume calculations in concrete, asphalt and other mixture proportioning purposes.|[0113] The fineness modulus property is defined in ASTM C 136, “Standard Test Method for Sieve Analysis of Fine and Coarse Aggregates,” and calculated “by adding the total percentages of material in a sample that is coarser than each of the following sieves (cumulative percentages retained), and dividing the sum by 100: 150-μm (No. 100), 300-μm (No. 50), 600-μm (No. 30), 1.18-mm (No. 16), 2.36-mm (No. 8), 4.75-mm (No. 4), 9.5-mm (⅜-in.), 19.0-mm (¾-in.), 37.5-mm (1½-in.) and larger increasing in the ratio of 2:1.” In this study, the sieves conclude at 19.0-mm (¾-in.) because this was the planned top-size of the aggregates. The fineness modulus property is used primarily as an indication of aggregate relative fineness or coarseness. The higher the fineness modulus value, the coarser the aggregate. Fineness modulus ranged from a low of 4.15 for LKD with air based aggregate to a high of 6.42 for the Slag with air based aggregate.|[0114] The staining test, defined by ASTM C 641, “Standard Test Method for Iron Staining Materials in Lightweight Concrete Aggregates,” provides a visual colorimetric method that was used to determine the iron staining potential of the nine by-product-based aggregates. The test involves selecting two-100 gm samples of aggregate with a specific gradation passing the % in (9.5 mm) sieve and retained on the No. 30 (600 μm) sieve. The sample is then placed at a uniform thickness on a white-filter paper that is then wrapped with cheesecloth. The wrapped sample was saturated in distilled water, and placed in a steam bath for 16 hours of continuous exposure. The sample was then removed from the filter paper, and the filter paper was oven dried on a watch glass. In this case, all of the samples tested had no staining with a rating of zero.|[0115] TABLE 19 Physical Properties of By-Product-Based Aggregates DensityAbsorptionSpecificFineness  (lb/ft3)(%)GravityModulusStaining  CKD + AIR46.641.60.994.980CKD + CO245.248.71.014.820CKD + FG46.044.20.955.110LKD + AIR56.031.40.994.150LKD + CO261.827.31.345.490LKD + FG48.825.71.205.170SLG + AIR44.133.01.246.420SLG + CO249.818.11.546.370SLG + FG46.927.01.246.390 |[0116] In Table 20, the by-product-based crushed aggregates range of values for the five physical properties are compared to published values for natural crushed gravel, two sources of pumice, and a source of manufactured expanded shale aggregate. The physical properties comparisons show that these aggregates are similar to expanded shale aggregates which fall in density below normal crushed gravel aggregate and just higher than pumice lightweight aggregate.|[0117] TABLE 20 Physical Properties Comparison of By-Product Mineral BasedAggregates to Commercial Materials DensityAbsorptionSpecificFineness  (lb/ft3)(%)GravityModulusStaining  Pumice55.016.31.203.100Volcanic37.032.10.762.55—PumiceExpanded54.018.01.733.880ShaleCrushed113.01.62.572.82—GravelRange for44.1-61.818.1-48.70.95-1.544.15-6.420By-ProductAggregatesTested |10. Actual and Potential Sequestration of Carbon Dioxide in the CLSM|[0118] Previously presented data illustrate that the foamed CLSM can sequester significant amounts of CO2 gas. Table 21 shows the average net % CO2 that was sequestered and stored for the three by-product based foamed CLSM during the 182-day course of the example studies. Net % CO2 sequestered was calculated by subtracting the average starting % CO2 by mass of each starting material from the % CO2 by mass of the by-product based foamed CLSM after 182 days.|[0119] TABLE 21 Average CO2 Sequestered by Percent Mass at 182 Day Age Total % CO2 by MassStarting % CO2Net % CO2Materialat 182-Day Ageby Mass at Day 0Sequestered CKD20.39.510.8LKD25.722.23.5Slag5.01.43.6 |[0120] Table 22 provides estimates based on the net % CO2 sequestered values shown in Table 21 of the amount of CO2 that the three by-product based foamed CLSM could potentially sequester, assuming that all of the three by-products produced in the United States were converted to the foamed CLSM of the present invention. In addition to what can be sequestered permanently in the mineral matrix of the CLSM, the process of the invention avoids CO2 production. Natural lightweight aggregate requires a quarry operation. Fired lightweight aggregate requires fuel consumption and additional CO2 emissions.|[0121] TABLE 22 Annual CO2 Sequestration Potential of By-Product Mineral Aggregates     Total CO2   Annual CO2 ContainedBy-ProductAnnual SequestrationTotal CO2inMineralProduction% CO2 byPotential% by Mass inAggregatesAggregate(tons)Mass(tons)Aggregates(tons) CKD20,000,00010.82,200,00020.34,050,000LKD2,800,0003.597,00025.7710,000Slag23,700,0003.6850,0005.01,200,000Total46,500,000—3,147,000—5,940,000 |[0122] Table 23 provides the data, calculations, and assumptions underlying another, more detailed estimate of the potential amount of CO2 that could be sequestered by cement-kiln dust based foamed CLSM.|[0123] TABLE 23 Cement Kiln Dust: Calcium Compound Reactions Assumptions:  49.76% by wt of Cement Kiln Dust (CKD) is“CaO”4.976% by wt of CKD is free CaO0.000887304mol CaO/1 g of CKD10% of “CaO” is free CaO (4.976%/49.76%)molar weight of CaO = 56.08 g/mol50% of “CaO” is 2CaO*SiO20.002218260mol 2CaO*SiO2/1 g of CKD50% * .4976 g of “CaO” in 2CaO*SiO2 per 1 g ofCKD2 moles of CaO per mol 2CaO*SiO230% of “CaO” is 3CaO*Al2O30.000887304mol 3CaO*Al2O3/1 g of CKD30% * .4976 g of “CaO” in 3CaO*Al2O3 per 1 gof CKD3 moles of CaO per mol 3CaO*Al2O3rest of “CaO” in forms that do not react toproduce or consume Ca(OH)2Rxns: (assume all are 90% complete)CaO + H2O → Ca(OH)20.000798573mol Ca(OH)2 produced from CaO/1 g  of CKD2(2CaO*SiO2) + 4H2O → 3CaO*2SiO2*3H2O + Ca(OH)20.000998217mol Ca(OH)2 produced from  2CaO*SiO2/1 g of CKD3CaO*Al2O3 + 12H2O + Ca(OH)2 → 3CaO*Al2O3*Ca(OH)2*12H2O0.000798573mol Ca(OH)2 consumed by  3CaO*Al2O3/1 g of CKDCa(OH)2 + CO2 → CaCO3 + H2O0.000898395mol CO2 consumed/1 g of CKD 0.039538371g of CO2 consumed/1 g of CKD Cement Kiln Dust: Sodium Compound Reactions Assumptions:  0.9% by wt of Cement Kiln Dust (CKD) is“Na2O”50% of “Na2O” is Na2O27.26041E−05mol Na2O2/1 g of CKD50% * .009 g of “Na2O” in Na2O2 per 1 g of CKD1 mol of Na2O per mol Na2O2molar weight Na2O = 61.98 g/molrest of “Na2O” in forms that do not react to produce or consumeCa(OH)2Rxns: (assume all are 90% complete)2Na2O2 + 2H2O → 4NaOH + O20.000130687mol NaOH produced/1 g of CKDNaOH + CO2 → NaHCO30.000117619mol CO2 consumed/1 g of CKD 0.005176394g of CO2 consumed/1 g of CKD Cement Kiln Dust: Potassium Compound Reactions Assumptions:  3.8% by wt of Cement Kiln Dust (CKD) is “K2O”30% of “K2O” is K2O20.000121019mol K2O2/1 g of CKD30% * 0.038 g of “K2O” in K2O2 per 1 g of CKD1 mol of K2O per mol K2O2molar weight K2O = 94.2 g/mol30% of “K2O” is KO20.000242038mol KO2/1 g of CKD30% * .038 g of “K2O” in KO2 per 1 g CKD0.5 mol of K2O per mol KO2molar weight K2O = 94.2 g/molrest of “Na2O” in forms that do not react toproduce or consume Ca(OH)2Rxns: (assume all are 90% complete)2K2O2 + 4H2O → 4KOH + O20.000217834mol KOH produced/1 g of CKD4KO2 + 2H2O → 4KOH + 3O20.000217834mol KOH produced/1 g of CKD2KOH + CO2 → K2CO3 + H2O0.000196051mol CO2 consumed/1 g of CKD 0.008628203g of CO2 consumed/1 g CKD Cement Kiln Dust: Magnesium Compound Reactions Assumptions:  2.23% by wt of Cement Kiln Dust (CKD) is “MgO”50% of “MgO” is available as Mg0.000285289mol Mg/1 g of CKD50% * .023 g of “MgO” in Mg per 1 g of CKD1 mol of MgO per mol Mgmolar weight MgO = 40.31 g/molrest of “MgO” in forms that do not react toproduce or consume Ca(OH)2Rxns: (assume all are 90% complete)Mg + 2H2O → Mg(OH)2 + H20.000256760mol Mg(OH)2 produced/1 g of CKDMg(OH)2 + CO2 → MgCO3 + H2O0.000231084mol CO2 consumed/1 g of CKD 0.010170011g of CO2 consumed/1 g of CKD Cement Kiln Dust: Total CO2 Consumed (sequestered) in CLSM  0.040g of CO2 consumed (sequestered)/g of CKD in Ca reactions 0.005g of CO2 consumed (sequestered)/g of CKD in Na reactions 0.009g of CO2 consumed (sequestered)/g of CKD in K reactions 0.010g of CO2 consumed (sequestered)/g of CKD in Mg reactions 0.064g of CO2 consumed (sequestered)/g of CKD TOTAL Assumptions:  1625lb of CKD/1 yd3 CLSM Sufficient CO2 and H2O so that neither limit the reaction 2225lb of CLSM/1 yd3 CLSM 103lb of CO2 consumed (sequestered)/yd3 of CLSM 0.046lb of CO2 consumed (sequestered)/lb of CLSM Annual sequestration estimate  Assumptions: 100000tons of CKD utilized for CLSM 123000yd3 CLSM produced 6350tons of CO2 consumed (sequestered) annually  |[0124] Table 24 provides the data, calculations, and assumptions underlying another, more detailed estimate of the potential amount of CO2 that could be sequestered by lime-kiln dust based foamed CLSM.|[0125] TABLE 24 Lime Kiln Dust: Calcium Compound Reactions Assumptions:  32.69% by wt of Lime Kiln Dust (LKD) is “CaO”  3.27% by wt of LKD is free CaO0.000583096mol CaO/1 g of LKD10% of “CaO” is free CaO (3.27%/32.7%)  molar weight of CaO = 56.08 g/mol  50% of “CaO” is 2CaO*SiO20.001457739mol 2CaO*SiO2/1 g of LKD50% * .327 g of “CaO” in 2CaO*SiO2 per 1 g of  LKD  2 moles of CaO per mol 2CaO*SiO2  30% of “CaO” is 3CaO*Al2O30.000583096mol 3CaO*Al2O3/1 g of LKD30% * .327 g of “CaO” in 3CaO*Al2O3 per 1 g of  LKD  3 moles of CaO per mol 3CaO*Al2O3  rest of “CaO” in forms that do not react to  produce or consume Ca(OH)2  Rxns: (assume all are 90% complete)  CaO + H2O → Ca(OH)20.000524786mol Ca(OH)2 produced from CaO/1 g  of LKD2(2CaO*SiO2) + 4H2O → 3CaO*2SiO2*3H2O + Ca(OH)20.000655983mol Ca(OH)2 produced from  2CaO*SiO2/1 g of LKD3CaO*Al2O3 + 12H2O + Ca(OH)2 → 3CaO*Al2O3*Ca(OH)2*12H2O0.000524786mol Ca(OH)2 consumed by  3CaO*Al2O3/1 g of LKDCa(OH)2 + CO2 → CaCO3 + H2O0.000590384mol CO2 consumed/1 g of LKD 0.025982812g of CO2 consumed/1 g of LKD Lime Kiln Dust: Sodium Compound Reactions Assumptions:  1.5% by wt of Lime Kiln Dust (LKD) is “Na2O”  50% of “Na2O” is Na2O20.000121007mol Na2O2/1 g of LKD50% * .015 g of “Na2O” in Na2O2 per 1 g of LKD  1 mol of Na2O per mol Na2O2  molar weight Na2O = 61.98 g/mol  rest of “Na2O” in forms that do not react to  produce or consume Ca(OH)2  Rxns: (assume all are 90% complete)  2Na2O2 + 2H2O → 4NaOH + O20.000217812mol NaOH produced/1 g of LKDNaOH + CO2 → NaHCO30.000196031mol CO2 consumed/1 g of LKD 0.008627323g of CO2 consumed/1 g of LKD Lime Kiln Dust: Potassium Compound Reactions Assumptions:  0.83% by wt of Lime Kiln Dust (LKD) is “K2O”  30% of “K2O” is K2O22.64331E−05mol K2O2/1 g of LKD30% * .0083 g of “K2O” in K2O2 per 1 g of LKD  1 mol of K2O per mol K2O2  molar weight K2O = 94.2 g/mol  30% of “K2O” is KO25.28662E−05mol KO2/1 g of LKD30% * .0083 g of “K2O” in KO2 per 1 g of LKD  0.5 mol of K2O per mol KO2  molar weight K2O = 94.2 g/mol  rest of “Na2O” in forms that do not react to  produce or consume Ca(OH)2  Rxns: (assume all are 90% complete)  2K2O2 + 4H2O → 4KOH + O24.75796E−05mol KOH produced/1 g of LKD4KO2 + 2H2O → 4KOH + 3O24.75796E−05mol KOH produced/1 g of LKD2KOH + CO2 → K2CO3 + H2O4.28217E−05mol CO2 consumed/1 g of LKD 0.001884581g of CO2 consumed/1 g of LKD Lime Kiln Dust: Magnesium Compound Reactions Assumptions:  24.9% by wt of Lime Kiln Dust (LKD) is “MgO”  50% of “MgO” is available as Mg0.003088564mol Mg/1 g of LKD50% * .249 g of “MgO” in Mg per 1 g of LKD  1 mol of MgO per mol Mg  molar weight MgO = 40.31 g/mol  rest of “MgO” in forms that do not react to  produce or consume Ca(OH)2  Rxns: (assume all are 90% complete)  Mg + 2H2O → Mg(OH)2 + H20.002779707mol Mg(OH)2 produced/1 g of LKDMg(OH)2 + CO2 → MgCO3 + H2O0.002501737mol CO2 consumed/1 g of LKD 0.110101425g of CO2 consumed/1 g of LKD Lime Kiln Dust: Total CO2 Consumed (sequestered) in CLSM  0.026g of CO2 consumed (sequestered)/g of LKD in Ca reactions 0.009g of CO2 consumed (sequestered)/g of LKD in Na reactions 0.002g of CO2 consumed (sequestered)/g of LKD in K reactions 0.110g of CO2 consumed (sequestered)/g of LKD in Mg reactions 0.147g of CO2 consumed (sequestered)/g of LKD TOTAL Assumptions:  1450lb of LKD/1 yd3 CLSM Sufficient CO2 and H2O so that neither limit the reaction  2050lb of CLSM/1 yd3 CLSM 213lb of CO2 consumed (sequestered)/yd3 of CLSM 0.104lb of CO2 consumed (sequestered)/lbof CLSM Annual sequestration estimate  Assumptions:  100000tons of LKD utilized for CLSM 138000yd3 CLSM produced 14670tons of CO2 consumed (sequestered) annually |[0126] Table 25 provides the data, calculations, and assumptions underlying another, more detailed estimate of the potential amount of CO2 that could be sequestered by slag cement based foamed CLSM.|[0127] TABLE 25 Blast Furnace Slag: Calcium Compound Reactions Assumptions:  38.15% by wt of Blast Furnace Slag (Slag) is“CaO”3.8% by wt of Slag is free CaO0.000677603mol CaO/1 g of Slag10% of “CaO” is free CaO (3.8%/38%)molar weight of CaO = 56.08 g/mol50% of “CaO” is 2CaO*SiO20.000169401mol 2CaO*SiO2/1 g of Slag50% * .038 g of “CaO” in 2CaO*SiO2 per 1 g ofSlag2 moles of CaO per mol 2CaO*SiO230% of “CaO” is 3CaO*Al2O36.77603E−05mol 3CaO*Al2O3/1 g of Slag30% * .038 g of “CaO” in 3CaO*Al2O3 per 1 g ofSlag3 moles of CaO per mol 3CaO*Al2O3rest of “CaO” in forms that do not react toproduce or consume Ca(OH)2Rxns: (assume all are 90% complete)CaO + H2O → Ca(OH)20.000609843mol Ca(OH)2 produced from CaO/1 g  of Slag2(2CaO*SiO2) + 4H2O → 3CaO*2SiO2*3H2O + Ca(OH)27.62304E−05mol Ca(OH)2 produced from  2CaO*SiO2/1 g of Slag3CaO*Al2O3 + 12H2O + Ca(OH)2 → 3CaO*Al2O3*Ca(OH)2*12H2O6.09843E−05mol Ca(OH)2 consumed by  3CaO*Al2O3/1 g of SlagCa(OH)2 + CO2 → CaCO3 + H2O0.00056258mol CO2 consumed/1 g of Slag 0.024759156g of CO2 consumed/1 g of Slag Blast Furnace Slag: Sodium Compound Reactions Assumptions:  0.0% by wt of Slag is “Na2O”50% of “Na2O” is Na2O20mol Na2O2/1 g of Slag50% * .00 g of “Na2O” in Na2O2 per 1 g of Slag1 mol of Na2O per mol Na2O2molar weight Na2O = 61.98 g/molrest of “Na2O” in forms that do not react to produce orconsume Ca(OH)2Rxns: (assume all are 90% complete)2Na2O2 + 2H2O → 4NaOH + O20mol NaOH produced/1 g of SlagNaOH + CO2 → NaHCO30mol CO2 consumed/1 g of Slag 0g of CO2 consumed/1 g of Slag Blast Furnace Slag: Potassium Compound Reactions Assumptions:  0.35% by wt of Slag is “K2O”30% of “K2O” is K2O21.11465E−05mol K2O2/1 g of Slag30% * .0035 g of “K2O” in K2O2 per 1 g of Slag1 mol of K2O per mol K2O2molar weight K2O = 94.2 g/mol30% of “K2O” is KO22.2293E−05mol KO2/1 g of Slag30% * .0035 g of “K2O” in KO2 per 1 g of Slag0.5 mol of K2O per mol KO2molar weight K2O = 94.2 g/molrest of “Na2O” in forms that do not react toproduce or consume Ca(OH)2Rxns: (assume all are 90% complete)2K2O2 + 4H2O → 4KOH + O22.00637E−05mol KOH produced/1 g of Slag4KO2 + 2H2O → 4KOH + 3O22.00637E−05mol KOH produced/1 g of Slag2KOH + CO2 → K2CO3 + H2O1.80573E−05mol CO2 consumed/1 g of Slag 0.000794703g of CO2 consumed/1 g of Slag Blast Furnace Slag: Magnesium Compound Reactions Assumptions:  11.02% by wt of Slag is “MgO”50% of “MgO” is available as Mg0.001366906mol Mg/1 g of Slag50% * .1102 g of “MgO” in Mg per 1 g of Slag1 mol of MgO per mol Mgmolar weight MgO = 40.31 g/molrest of “MgO” in forms that do not react toproduce or consume Ca(OH)2Rxns: (assume all are 90% complete)Mg + 2H2O → Mg(OH)2 + H20.001230216mol Mg(OH)2 produced/1 g of SlagMg(OH)2 + CO2 → MgCO3 + H2O0.001107194mol CO2 consumed/1 g of Slag 0.048727619g of CO2 consumed/1 g of Slag Blast Furnace Slag: Total CO2 Consumed (sequestered) in CLSM  0.025g of CO2 consumed (sequestered)/g of Slag in Ca reactions 0.000g of CO2 consumed (sequestered)/g of Slag in Na reactions 0.001g of CO2 consumed (sequestered)/g of Slag in K reactions 0.049g of CO2 consumed (sequestered)/g of Slag in Mg reactions 0.074g of CO2 consumed (sequestered)/g of Slag TOTAL Assumptions:  1683lb of of Slag/1 yd3 CLSM Sufficient CO2 and H2O so that neither limit the reaction 2283lb of CLSM/1 yd3 CLSM 125lb of CO2 consumed (sequestered)/yd3 of CLSM 0.055lb of CO2 consumed (sequestered)/lb of CLSM Annual Sequestration estimate  Assumptions: 100000tons of Slag 119000yd3 CLSM produced 7440tons of CO2 consumed (sequestered) annually  |[0128] Thus, the invention provides products and processes that make environmentally beneficial use of the carbon dioxide produced as by-products of the combustion of fossil fuels in the combustion chambers of power and industrial production plants, the cement-kiln dust produced as a by-product of portland cement production, the lime-kiln dust produced as a by-product of lime production, and the slag cement produced as a by-product of iron and steel production. In the process, a foam including a foaming agent and flue gas including carbon dioxide is formed, and the foam is added to a mixture including a cementitious material (e.g., cement-kiln dust, lime-kiln dust, or slag cement) and water to form a foamed mixture. Thereafter, the foamed mixture is allowed to set, preferably to a controlled low-strength material having a compressive strength of 1200 psi or less. The carbon dioxide in the flue gas reacts with hydration products in the controlled low-strength material and in turn sequesters the carbon dioxide.|[0129] Although the present invention has been described in considerable detail with reference to certain embodiments, one skilled in the art will appreciate that the present invention can be practiced by other than the described embodiments, which have been presented for purposes of illustration and not of limitation. Therefore, the scope of the appended claims should not be limited to the description of the embodiments contained herein.|INDUSTRIAL APPLICABILITY|[0130] The invention relates to a process for sequestering carbon dioxide through the production of lightweight controlled low-strength materials. In one process of the invention, carbon dioxide from the flue gas of a coal combustion chamber is sequestered. In the process, a foam including a foaming agent and the flue gas is formed, and the foam is added to a mixture including a cementitious material (e.g., cement-kiln dust, lime-kiln dust, or slag cement) and water to form a foamed mixture. Thereafter, the foamed mixture is allowed to set into a controlled low-strength material in which the carbon dioxide is sequestered. Family Number|(4099265)|4099265|Abstract|(CA2537383 C)|A process for sequestering carbon dioxide from the flue gas emitted from a combustion chamber is disclosed. In the process, a foam including a foaming agent and the flue gas is formed, and the foam is added to a mixture including a cementitious material (e.g., fly ash) and water to form a foamed mixture. Thereafter, the foamed mixture is allowed to set, preferably to a controlled low- strength material having a compressive strength of 1200 psi or less. The carbon dioxide in the flue gas and waste heat reacts with hydration products in the controlled low-strength material to increase strength. In this process, the carbon dioxide is sequestered. The CLSM can be crushed or pelletized to form a lightweight aggregate with properties similar to the naturally occurring mineral, pumice.|(US7390444 B2)|A process for sequestering carbon dioxide from the flue gas emitted from a combustion chamber is disclosed. In the process, a foam including a foaming agent and the flue gas is formed, and the foam is added to a mixture including a cementitious material (e.g., fly ash) and water to form a foamed mixture. Thereafter, the foamed mixture is allowed to set, preferably to a controlled low-strength material having a compressive strength of 1200 psi or less. The carbon dioxide in the flue gas and waste heat reacts with hydration products in the controlled low-strength material to increase strength. In this process, the carbon dioxide is sequestered. The CLSM can be crushed or pelletized to form a lightweight aggregate with properties similar to the naturally occurring mineral, pumice.|CPC codes|(CA2537383 C)|B01D-053/62|(US7390444 B2)|B01D-053/62|(US9028607 B2)|B01D-053/62|B01D-2251/404|B01D-2257/504|B01D-2259/80|IPC codes|(CA2537383 C)|B01D-053/62|(US9028607 B2)|B01D-053/62|Title|(CA2537383 C)|Carbon Dioxide Sequestration in Foamed Controlled Low Strength Materials|(CA2537383 A1)|Carbon Dioxide Sequestration in Foamed Controlled Low Strength Materials|(US7390444 B2)|Carbon Dioxide Sequestration in Foamed Controlled Low Strength Materials|(US20060185560 A1)|Carbon Dioxide Sequestration in Foamed Controlled Low Strength Materials|(US9028607 B2)|Carbon Dioxide Sequestration in Foamed Controlled Low Strength Materials|(US20080245274 A1)|Carbon Dioxide Sequestration in Foamed Controlled Low Strength Materials| Environmental technology|Materials, metallurgy|Other special machines 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US6153005; US6648949; US4362679; US6162839; US6334895; US-109669; US-128980; US-591168; US1449696; US1966419; US1966864; US3867159; US4069063; US4093690; US4117060; US4350567; US4362679; US4374672; US4383862; US4407676; US4415366; US4427610; US4872913; US4900359; US5013157; US5051217; US5307876; US5397553; US5435843; US5518540; US5650562; US5654352; US5690729; US5897704; US5918429; US5951751; US5965201; US6153005; US6235092; US6264736; US6352576; US6372023; US6387174; US6461424; US6521021; US6569388; US6648949; CH-644828; DE4207235; JP02018368; JP06263562 (US9028607)|Applicant references|-ASTM C 618, "Standard Specification for Fly Ash and Raw or Calcined Natural Pozzolan for Use as a Mineral Admixture in Portland Cement Concrete", 1999.|-American Concrete Institute Committee 229, "Controlled Low-Strength Materials", ACI 229R-99, pp. 229R-1 to 229R-15, Jun. 1999.||(US7390444)|Applicant references|-ASTM C 618, "Standard Specification for Fly Ash and Raw or Calcined Natural Pozzolan for Use as a Mineral Admixture in Portland Cement Concrete", 1999.|-American Concrete Institute Committee 229, "Controlled Low-Strength Materials", ACI 229R-99, pp. 229R-1 to 229R-15, Jun. 1999.|| LAPSED (US9028607)|LAPSED|(US7390444)|LAPSED|(CA2537383)|LAPSED DEAD (US9028607)|DEAD|(US7390444)|DEAD|(CA2537383)|DEAD (US9028607)|LEGAL DETAILS FOR US9028607|Actual or expected expiration date=2023-06-19|Legal state=DEAD|Status=LAPSED|Event publication date=2008-06-12|Event code=US/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=US US12138019|Application date=2008-06-12|Standardized application number=2008US-12138019|Event publication date=2008-06-12|Event code=US/EXMR|Event group=Administrative notifications|USPTO Examiner Name|PRIMARY EXAMINER:HIJJI, KARAM Y|Event publication date=2008-06-12|Event code=US/ART|Event group=Administrative notifications|USPTO Art Group|ART=1731|Event publication date=2008-06-12|Event code=US/DK|Event group=Examination events|Attorney Docket Number|Docket Nbr: 960049.00078|Event publication date=2008-06-12|Event code=US/CUST|Event group=Examination events|Attorney/Agent Customer Number|Customer Nbr: 26710|Event publication date=2008-06-12|Event code=US/ENT|Event group=Administrative notifications|Entity Status Set to Undiscounted|Business Entity Status: Regular Undiscounted|Event publication date=2008-06-12|Event code=US/AIA|Event group=Administrative notifications|First Inventor File Indicated:|AIA=No|Event publication date=2008-06-26|Event code=US/APPFILEREC|Event group=Administrative notifications OAO|Filing Receipt|Event publication date=2008-10-08|Event code=US/DISCSEF|Event group=OAI|Electronic Information Disclosure Statement|Event publication date=2008-10-08|Event code=US/IDS|Event group=Examination events OAI|Information Disclosure Statement Filed|Event publication date=2008-10-09|Event code=US/A1|Event group=Examination events|Application published|Publication country=US|Publication number=US20080245274|Publication stage code=A1|Publication date=2008-10-09|Standardized publication number=US20080245274|Event publication date=2008-10-09|Event code=US/PGPUBN|Event indicator=Pos|Event group=Examination events OAO|PG-Pub Issue Notification|Event publication date=2008-10-13|Event code=US/AS|Event group=Change of name or address Reassignment|Assignment|ASSIGNMENT OF ASSIGNORS INTEREST|Assignor:RAMME, BRUCE W.|Reel/frame:021674/0244|OWNER:WISCONSIN ELECTRIC POWER COMPANY, WISCONSIN|Effective date of the event=2008-10-09|Event publication date=2009-02-18|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2010-10-06|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2010-10-14|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2011-01-19|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2011-02-14|Event code=US/CTNF|Event group=Examination events OA OAO|Non-Final Rejection|Event publication date=2011-02-18|Event code=US/112NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 112 - subject matter in claims not properly defined|RJD=2011-02-18|R4R=112|RJST=non-final|Rejected claims 26-28|Event publication date=2011-02-18|Event code=US/103NF|Event indicator=Neg|Event group=Examination events|Non-final rejection reason 103 - obvious subject matter in claims|RJD=2011-02-18|R4R=103a|RJST=non-final|Rejected claims 1-28|RJCT=US6334895|RJCT=US6046255|RJCT=US5634972|RJCT=US5935317|RJCT=US20080178770|Event publication date=2011-02-18|Event code=US/DBLNF|Event indicator=Neg|Event group=Examination events|Non-final rejection - Double Patenting|RJD=2011-02-18|R4R=DBL|RJST=non-final|Rejected claims 1-16, 20-23, and 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publication date=2015-04-08|Event code=US/N084|Event group=Payment or non-payment notifications|Issue Fee Payment Verified|Event publication date=2015-04-08|Event code=US/IFEE|Event group=Payment or non-payment notifications|Issue Fee Payment Received|Event publication date=2015-04-09|Event code=US/APRDY|Event indicator=Pos|Event group=Examination events|Application Is Considered Ready for Issue|Event publication date=2015-04-22|Event code=US/ISSM|Event indicator=Pos|Event group=Examination events OAO Restitution or restoration|Issue Notification Mailed|Event publication date=2015-05-12|Event code=US/B2|Event indicator=Pos|Event group=Event indicating In Force|Granted patent as second publication|Publication country=US|Publication number=US09028607|Publication stage code=B2|Publication date=2015-05-12|Standardized publication number=US9028607|Event publication date=2015-05-12|Event code=US/354|Event indicator=Pos|Event group=Extension of term of duration of protection|Patent term extended under 35 U.S.C 154(b) until/for|Extension Type=PTA|Delays (A,B,C): 1985 Overlap Delays: 0 Non Overlap Delays: 0|PTO Office Delays: 0 Applicant Delays: 91 Adjustment total: |Number of days of extension=1894|Event publication date=2015-05-12|Event code=US/PTA36|Event group=Extension of term of duration of protection|PTA 36 Months|Action Recorded:|RECD=2015-05-12|Event publication date=2018-05-22|Event code=US/NMFP|Event group=Payment or non-payment notifications|Publication of First Notice of Maintenance Fees Payable.|Year of payment of annual fees=3|Event publication date=2018-11-01|Event code=US/MAFP|Event indicator=Pos|Event group=Payment or non-payment notifications|Maintenance Fee Payment|Annual fees payment date=2018-11-01|Year of payment of annual fees=4|PAYMENT OF MAINTENANCE FEE, 4TH YEAR, LARGE ENTITY (ORIGINAL EVENT CODE: M1551)|Entity status of patent owner: LARGE ENTITY|Event publication date=2018-11-01|Event code=US/M1551|Event group=Payment or non-payment 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date=2008-06-24|Event code=US/B2|Event indicator=Pos|Event group=Event indicating In Force|Granted patent as second publication|Publication country=US|Publication number=US07390444|Publication stage code=B2|Publication date=2008-06-24|Standardized publication number=US7390444|Event publication date=2008-06-24|Event code=US/354|Event indicator=Pos|Event group=Extension of term of duration of protection|Patent term extended under 35 U.S.C 154(b) until/for|Extension Type=PTA|Delays (A,B,C): 533 Overlap Delays: 0 Non Overlap Delays: 0|PTO Office Delays: 0 Applicant Delays: 30 Adjustment total: |Number of days of extension=503|Event publication date=2011-07-05|Event code=US/NMFP|Event group=Payment or non-payment notifications|Publication of First Notice of Maintenance Fees Payable.|Year of payment of annual fees=3|Event publication date=2011-09-19|Event code=US/FPAY|Event indicator=Pos|Event group=Event indicating In Force Payment or non-payment notifications|Fee payment recorded|Annual 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https://data.uspto.gov/patent-file-wrapper/search/details/12138019/application-data https://permalink.orbit.com/RenderStaticFirstPage?XPN=ufWaRDTS8fHdGqGyRhNS9XfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT US (US9028607)|US|(CA2537383)|US|(CA2537383)|US|(US7390444)|US (US9028607)|NAME=Wisconsin Electric Power Company , CITY=Milwaukee , STATE=WI , COUNTRY=US , ATYP=US Company|(CA2537383)|NAME=WISCONSIN ELECTRIC POWER COMPANY 231 W. Michigan Avenue , CITY=MILWAUKEE , STATE=WI , POSTCODE=53201 , COUNTRY=US|(CA2537383)|NAME=WISCONSIN ELECTRIC POWER COMPANY 231 W. Michigan Avenue, MILWAUKEE, WI, 53201 , COUNTRY=US|(US7390444)|NAME=Wisconsin Electric Power Company , CITY=Milwaukee , STATE=WI , COUNTRY=US , ATYP=US Company |(US20080245274)|US||(US20060185560)|US|(CA2537383)|CA| (US9028607)|NAME=Quarles & Brady LLP|(US20080245274)|NAME=QUARLES & BRADY LLP 411 E. WISCONSIN AVENUE, SUITE 2040 , CITY=MILWAUKEE , STATE=WI , POSTCODE=53202-4497 , COUNTRY=US|(US7390444)|NAME=Quarles & Brady LLP|(US20060185560)|NAME=QUARLES & BRADY LLP 411 E. WISCONSIN AVENUE SUITE 2040 , CITY=MILWAUKEE , STATE=WI , POSTCODE=53202-4497 , COUNTRY=US|(CA2537383)|NAME=LAVERY, DE BILLY, LLP , COUNTRY=CA|(CA2537383)|NAME=GOUDREAU GAGE DUBUC (US9028607)|US|(US20080245274)|US|(US7390444)|US; US; US|(US20060185560)|US; US; US|(CA2537383)|US; US; US|(CA2537383)|US; US; US (US9028607)|NAME=Ramme Bruce W., CITY=Okauchee, STATE=WI , COUNTRY=US|(US20080245274)|NAME=Ramme Bruce W., CITY=Okauchee, STATE=WI , COUNTRY=US|(US7390444)|NAME=Ramme Bruce W., CITY=Okauchee, STATE=WI , COUNTRY=US |NAME=Goeckner Bryna D., CITY=Whitefish Bay, STATE=WI , COUNTRY=US |NAME=Russart Joshua J., CITY=Dousman, STATE=WI , COUNTRY=US|(US20060185560)|NAME=Ramme Bruce W., CITY=Okauchee, STATE=WI , COUNTRY=US |NAME=Goeckner Bryna D., CITY=Whitefish Bay, STATE=WI , COUNTRY=US |NAME=Russart Joshua J., CITY=Dousman, STATE=WI , COUNTRY=US|(CA2537383)|NAME=RAMME, BRUCE W., COUNTRY=US |NAME=GOECKNER, BRYNA DEVITT, COUNTRY=US |NAME=RUSSART, JOSHUA JOHN, COUNTRY=US|(CA2537383)|NAME=RAMME BRUCE W, COUNTRY=US |NAME=GOECKNER BRYNA DEVITT, COUNTRY=US |NAME=RUSSART JOSHUA JOHN, COUNTRY=US 40 2 Titre: (US9028607)|Carbon dioxide sequestration in foamed controlled low strength materials Résumé: (US9028607)|A process for sequestering carbon dioxide from the exhaust gas emitted from a combustion chamber is disclosed. In the process, a foam including a foaming agent and the exhaust gas is formed, and the foam is added to a mixture including a cementitious material (e.g., cement-kiln dust, lime kiln dust, or slag cement) and water to form a foamed mixture. Thereafter, the foamed mixture is allowed to set, preferably to a controlled low-strength material having a compressive strength of 1200 psi or less. The carbon dioxide in the exhaust gas reacts with hydration products in the controlled low-strength material and in turn sequesters the carbon dioxide. 54 Abstract gpt-4o-mini no The process described focuses on sequestering CO₂ from exhaust gases using cementitious materials, which falls outside the scope of accelerated weathering and mineral carbonation related to silicate or alkaline minerals.
55 CN202210712347 CN202210712347 CN114982414 101616186 CN114982414 A 2022-09-02 [CN114982414] 2022-06-22 2022-06-22 2022-09-02 (CN114982414)|2024-03-01 (CN114982414)|Method for improving carbon sequestration potential of soil by using organic fertilizer (CN114982414)|The invention discloses a method for improving the carbon sequestration potential of soil by using an organic fertilizer, and belongs to the technical field of soil improvement, and the method specifically comprises the following steps: 1) ridging in a soil carbon sequestration area, then burying biochar into furrows, then applying the organic fertilizer, and then planting green manure crops; and (2) after the green manure crops are harvested, crushing straws of the green manure crops, mixing the crushed straws with an organic fertilizer, flatly spraying the mixture on the ground, and deeply ploughing the soil, so that the crops can be planted. The organic fertilizer is matched with the biochar and green manure crops for use, the surface area of soil aggregate carbon sequestration is increased, the carbon sequestration capacity of soil is improved, meanwhile, the soil fertility and air permeability are improved, growth of crops is facilitated, and the yield of the crops can be remarkably increased. LIAONING AGRICULTURAL DEVELOPMENT SERVICE CENTER (CN114982414)|LIAONING AGRICULTURAL DEV SERVICE CENTER ([CN]) SONG DAN|WANG JILEI (CN114982414)|SONG DAN|WANG JILEI (CN114982414)|CHEN YUEXIA;BEIJING ORIENTAL SHENGFAN INTELLECTUAL PROPERTY AGENCY FIRM|Reg. Nb: 11562 (CN114982414)|However, the basic national situation of China is that many people have less land, and the rapid urbanization process causes a great reduction in the cultivated land and faces the dilemma of cultivated land loss and quality reduction.|The present invention will be described in further detail with reference to specific embodiments in order to make the above objects, features and advantages more apparent and understandable.|Therefore, how to provide a method capable of effectively improving the carbon sequestration potential of soil is a technical problem which needs to be solved urgently by the technical personnel in the field.| (CN114982414)|1. A method for improving the carbon sequestration potential of soil by using an organic fertilizer is characterized by comprising the following steps:1) ridging a soil carbon sequestration area, burying biochar into furrows, applying an organic fertilizer, and planting green manure crops;2) after the green manure crops are harvested, the straws are crushed, mixed with the organic fertilizer and then spread on the ground, and then the soil is turned deeply, so that the crops can be planted.| (CN114982414)|The invention aims to provide a method for improving the carbon sequestration potential of soil by utilizing an organic fertilizer, so as to solve the problems in the prior art. In order to achieve the purpose, the invention provides the following scheme:|The invention discloses a method for improving soil carbon sequestration potential by using an organic fertilizer, which belongs to the technical field of soil improvement and specifically comprises the following steps: 1) ridging in a soil carbon sequestration area, then burying biochar into furrows, applying an organic fertilizer, and then planting green manure crops; 2) after the green manure crops are harvested, the straws are crushed, mixed with organic fertilizer and then spread on the ground, and the soil is turned deeply, so that the crops can be planted.|The invention relates to the field of soil improvement, in particular to a method for improving the carbon sequestration potential of soil by using an organic fertilizer.| (CN114982414)|ORGANIC FERTILIZER(100,66)|GROUND(100,41)|CARBON SEQUESTRATION(100,29)|GREEN MANURE CROP(100,17)|CULTIVATED LAND LOSS DILEMMA(60,1)|RAPID URBANIZATION(51,1)|MICROBIAL BACTERIUM(48,8)|SHEEP DUNG(45,17)|MICROORGANISM BACTERIA(41,2)|TECHNICAL PERSONNEL(41,1)|BASIC NATIONAL SITUATION(40,1)|BEAN CAKE(39,16)|PLANT STRAW(37,16)|FURROW(37,4)|SOIL CARBON SEQUESTRATION(36,3)|CULTIVATED LAND LOSS(36,1)|BURYING(35,4)|SOIL AGGREGATE(34,2)|STRAW(33,12)|PLANT ASH(31,16)|DEEP PLOWING DEPTH(31,8)|CROP(31,7)|ORGANIC FERTILIZER SPRAYING(31,1)|BACILLUS THURINGIENSIS(29,14)|SOIL IMPROVEMENT(29,2)|CULTIVATED LAND(29,1)|RIDGE SPACING(29,1)|SOIL CARBON SEQUESTRATION AREA(28,5)|SOIL CARBON SEQUESTRATION CAPACITY(26,3)|NEXT SEASON CROP(26,2)|HORIZONTAL SPRINKLING THICKNESS(25,1)|NOCARDIA(24,12)|BIOCHAR(24,9)|QUALITY REDUCTION(24,1)|COW DUNG(22,17)|SOIL FERTILITY(18,2)|RIDGE HEIGHT(17,4)|MISCANTHUS(16,3)|SESBANIA(15,4)|TAMARISK(15,3)|ALFALFA(14,4)|STRAW MIXING RATIO(14,3)|AIR PERMEABILITY(10,1)|CROP ROOT UPDATE(9,1)|RECLAIMED FARMLAND(9,1)|SOIL TREATMENT(8,3)|FLAT SPRINKLING FERTILIZER THICKNESS(8,2)|BURYING STRAW(8,1)|CRUSHED STRAW(8,1)|PLANTING VETCH(8,1)|SOIL IMPROVEMENT FIELD(8,1)|CORN PLANTING(7,1)|CREATIVE EFFORT(7,1)|PLANTING CORN(7,1)|SUN CURING FERMENTATION(7,1)|YEAR CORN YIELD(7,1)|BOTTOM WIDTH(6,4)|SOIL CARBON FIXATION(6,2)|SOIL CARBON SINK(6,2)|CARBON FIXATIONTHE(6,1)|RIDGE INTERVAL(6,1)|GROUND SURFACE(5,3)|CHARCOAL(5,2)|MICROORGANISM(5,2)|SOIL CARBON RESERVOIR(5,2)|BACTERIAL SPECIES RATIO(4,1)|BACTERIAL SPECIES SOURCE(4,1)|CHINESE SILVERGRASS(4,1)|FLAT SPRINKLING THICKNESS(4,1)|INOCULATION RATIO(4,1)|INOCULUM RATIO(4,1)|POTASSIUM COMPOUND FERTILIZER(4,1)| (CN114982414)|1. A method for improving the carbon sequestration potential of soil by using an organic fertilizer is characterized by comprising the following steps:|1) ridging a soil carbon sequestration area, burying biochar into furrows, applying an organic fertilizer, and planting green manure crops;|2) after the green manure crops are harvested, the straws are crushed, mixed with the organic fertilizer and then spread on the ground, and then the soil is turned deeply, so that the crops can be planted.|2. The method for improving the carbon sequestration potential of soil by using the organic fertilizer as claimed in claim 1, wherein the organic fertilizer in the steps 1) and 2) comprises the following raw materials in parts by weight:|20-55 parts of cow dung, 10-35 parts of sheep dung, 60-80 parts of plant straws, 15-20 parts of plant ash, 10-15 parts of bean cakes and 1-2 parts of microbial bacteria.|3. The method for improving the carbon sequestration potential of soil by utilizing the organic fertilizer as claimed in claim 2, wherein the microorganism bacteria comprise bacillus thuringiensis and nocardia, and the inoculation amount ratio of the bacillus thuringiensis to the nocardia is (3-7): 1.|4. The method for improving the carbon sequestration potential of soil by using the organic fertilizer as claimed in claim 1, wherein the application amount of the organic fertilizer in the step 1) is 65-80kg per mu.|5. The method for improving the carbon sequestration potential of soil by using the organic fertilizer as claimed in claim 1, wherein in the step 1), the ridge height of the ridge is 10-25cm, the bottom width is 55-65cm, and the ridge spacing is 50-60 cm.|6. The method for improving the carbon sequestration potential of soil by using the organic fertilizer as claimed in claim 1, wherein the biochar in the step 1) is prepared by using straws as a raw material; the green manure crops comprise one or more of vetch, alfalfa, tamarisk, sesbania and miscanthus.|7. The method for improving the carbon sequestration potential of the soil by using the organic fertilizer as claimed in claim 1, wherein the mixing ratio of the straw and the organic fertilizer in the step 2) is 1 (5-7).|8. The method for improving the carbon sequestration potential of the soil by utilizing the organic fertilizer as claimed in claim 1, wherein the thickness of the horizontal sprinkling in the step 2) is 5-10 cm; the deep ploughing depth is 20-50 cm.|9. The method for improving the carbon sequestration potential of soil by using the organic fertilizer as claimed in claim 1, further comprising the following steps of:|3) after harvesting the crops of the previous season every year, organic fertilizer is horizontally sprayed on the ground surface and deeply ploughed to soil, and then the crops of the next season are planted.|10. The method for improving the carbon sequestration potential of soil by using the organic fertilizer as claimed in claim 9, wherein the thickness of the horizontally sprayed organic fertilizer in the step 3) is 8-13 cm; the deep ploughing depth is 20-50 cm. (CN114982414)|TECHNICAL FIELD|[0001] The invention relates to the field of soil improvement, in particular to a method for improving the carbon sequestration potential of soil by using an organic fertilizer.|BACKGROUND ART|[0002] The soil carbon sink is an important path for reducing carbon emission and relieving global climate change. In the global carbon cycle, the soil carbon reservoir is 5 times as large as that of forests and other vegetation, and 3 times as large as that of atmospheric air. 60% of carbon in the soil carbon reservoir exists in soil in the form of organic matters, and the huge soil carbon storage amount is CO in the atmosphere 2 The level of (c) has a significant effect.|[0003] However, the basic national situation of China is that many people have less land, and the rapid urbanization process causes a great reduction in the cultivated land and faces the dilemma of cultivated land loss and quality reduction. The newly reclaimed farmland generally has the problem of low soil fertility, 80 percent of original organic carbon of surface soil is mineralized and decomposed in the soil disturbance process, and the organic carbon reserve of the soil is extremely low and is only 40-60 percent of that of a normal farmland.|[0004] Therefore, how to provide a method capable of effectively improving the carbon sequestration potential of soil is a technical problem which needs to be solved urgently by the technical personnel in the field.|DISCLOSURE|Disclosure of Invention|[0005] The invention aims to provide a method for improving the carbon sequestration potential of soil by utilizing an organic fertilizer, so as to solve the problems in the prior art.|[0006] In order to achieve the purpose, the invention provides the following scheme:|[0007] a method for improving the carbon sequestration potential of soil by using an organic fertilizer comprises the following steps:|[0008] 1) ridging a soil carbon sequestration area, burying biochar into furrows, applying an organic fertilizer, and planting green manure crops;|[0009] 2) after the green manure crops are harvested, the straws are crushed, mixed with organic fertilizer and then spread on the ground, and the soil is turned deeply, so that the crops can be planted.|[0010] Preferably, the organic fertilizer in the steps 1) and 2) comprises the following raw materials in parts by weight:|[0011] 20-55 parts of cow dung, 10-35 parts of sheep dung, 60-80 parts of plant straws, 15-20 parts of plant ash, 10-15 parts of bean cakes and 1-2 parts of microbial bacteria.|[0012] Preferably, the microorganism bacteria comprise bacillus thuringiensis and nocardia, and the ratio of the inoculation amount of the bacillus thuringiensis to the inoculation amount of the nocardia is (3-7): 1.|[0013] Preferably, the application amount of the organic fertilizer in the step 1) is 65-80kg per mu.|[0014] Preferably, the ridge height of the ridges in the step 1) is 10-25cm, the bottom width is 55-65cm, and the ridge distance is 50-60 cm.|[0015] Preferably, the biochar in the step 1) is prepared by taking straws as raw materials; the green manure crops comprise one or more of vetch, alfalfa, tamarisk, sesbania and miscanthus.|[0016] Preferably, the mixing ratio of the straws and the organic fertilizer in the step 2) is 1 (5-7).|[0017] Preferably, the thickness of the flat sprinkling in the step 2) is 5-10 cm; the deep ploughing depth is 20-50 cm.|[0018] Preferably, the method further comprises the following steps:|[0019] 3) after harvesting the crops in the previous season every year, flatly spraying organic fertilizer on the ground surface, deeply turning to soil, and then planting the crops in the next season.|[0020] Preferably, the thickness of the flat-sprinkling organic fertilizer in the step 3) is 8-13 cm; the deep ploughing depth is 20-50 cm.|[0021] The invention discloses a method for improving soil carbon sequestration potential by using an organic fertilizer, which improves the soil structure, increases the carbon sequestration surface area of soil aggregates, increases fertility, loosens the soil, improves the soil permeability, is beneficial to the update of crop roots and improves the carbon sequestration capacity of the soil. The simple substance carbon in the charcoal powder used in the invention can be fixed in the soil basically and irreversibly, thus increasing the carbon sink of the soil, and moreover, the charcoal has fluffy characteristic, so that the porosity structure of the soil can be increased rapidly, and the ventilation effect of the soil is improved. In addition, the green manure crops planted in the invention can provide fertilizer sources for crops and improve soil fertility, and after the straws and the organic fertilizer are deeply turned into the soil, the microorganisms in the organic fertilizer can promote the straws to be thoroughly decomposed, so that soil organic matters are further improved, the carbon sequestration capacity of the soil is improved, and the growth of the crops is facilitated.|INVENTION MODE|Detailed Description|[0022] The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.|[0023] The present invention will be described in further detail with reference to specific embodiments in order to make the above objects, features and advantages more apparent and understandable.|[0024] A method for improving the carbon sequestration potential of soil by using an organic fertilizer comprises the following steps:|[0025] 1) ridging in a soil carbon sequestration area, then burying biochar into furrows, applying an organic fertilizer, and then planting green manure crops;|[0026] 2) after the green manure crops are harvested, the straws are crushed, mixed with organic fertilizer and then spread on the ground, and the soil is turned deeply, so that the crops can be planted.|[0027] In some embodiments of the present invention, the organic fertilizer in steps 1) and 2) comprises the following raw materials in parts by weight:|[0028] 20-55 parts of cow dung, 10-35 parts of sheep dung, 60-80 parts of plant straws, 15-20 parts of plant ash, 10-15 parts of bean cakes and 1-2 parts of microbial bacteria. The conventional organic fertilizer has certain effect on improving the carbon sequestration potential of soil, but the further improvement is not easy on the basis, and the inventor finds that the improvement effect of different types of organic fertilizers on the carbon sequestration potential of soil is far from each other through experimental research, the different kinds of organic fertilizers are compounded in different proportions, so that the effect of improving the carbon fixation effect of the soil is far from each other, therefore, the invention creatively selects 20-55 parts of cow dung, 10-35 parts of sheep dung, 60-80 parts of plant straws, 15-20 parts of plant ash, 10-15 parts of bean cakes and 1-2 parts of microbial bacteria to form the compound organic fertilizer, when used alone, the organic fertilizer has no obvious difference with the conventional organic fertilizer of the same type in improving the soil carbon fixation effect, but when the fertilizer is used together with biochar and green manure crops, the soil carbon sequestration effect is obviously improved.|[0029] In some embodiments of the invention, the microorganism comprises bacillus thuringiensis and nocardia, and the ratio of the inoculum size of bacillus thuringiensis to nocardia is (3-7): 1.|[0030] The present invention is not particularly limited in the source of the bacterial species, and the bacterial species may be isolated by itself or purchased directly, and the technical effects of the present invention can be achieved as long as the ratio of the bacterial species to the inoculum size of Bacillus thuringiensis and Nocardia is (3-7): 1. In some embodiments of the invention, it is preferred to purchase Bacillus thuringiensis and Nocardia directly.|[0031] In some embodiments of the invention, the application amount of the organic fertilizer in the step 1) is 65-80kg per mu.|[0032] In some embodiments of the invention, the ridges in step 1) have a ridge height of 10-25cm, a bottom width of 55-65cm, and a ridge spacing of 50-60 cm.|[0033] If not specifically stated, the present invention does not specifically limit the type of the biochar, and optionally, the biochar is prepared from crop straws or forest, wood and grass, and in some embodiments of the present invention, the biochar in step 1) is prepared from straws as a raw material; the green manure crops comprise one or more of vetch, alfalfa, tamarisk, sesbania and miscanthus.|[0034] In some embodiments of the invention, the mixing ratio of the straws and the organic fertilizer in the step 2) is 1 (5-7).|[0035] If not specifically stated, the thickness of the flat sprinkling fertilizer is not particularly limited by the invention, and the conventional application amount of the organic fertilizer is met, and in some embodiments of the invention, the thickness of the flat sprinkling fertilizer in the step 2) is 5-10 cm; the depth of the deep ploughing is not particularly limited as long as the conventional application mode of the organic fertilizer is satisfied, and in some embodiments, the depth of the deep ploughing is preferably 20-50 cm.|[0036] In some embodiments of the invention, the method for improving the carbon sequestration potential of soil by using the organic fertilizer further comprises the following steps:|[0037] 3) after harvesting the crops of the previous season every year, organic fertilizer is horizontally sprayed on the ground surface and deeply ploughed to soil, and then the crops of the next season are planted.|[0038] The thickness of the flat spraying fertilizer is not particularly limited if not specifically stated, and the conventional application amount of the organic fertilizer is met, and in some embodiments of the invention, the thickness of the flat spraying organic fertilizer in the step 3) is 8-13 cm; the present invention has no particular limitation on the depth of the deep ploughing, unless otherwise specified, as long as the conventional application manner of the organic fertilizer is satisfied, and in some embodiments of the present invention, the depth of the deep ploughing in step 3) is preferably 20 to 50 cm.|[0039] The technical solution of the present invention will be described in detail below with reference to specific examples. The straw biochar in the following examples is biochar obtained by calcining corn straws. The specific preparation method is conventional technology, and is not described herein. The cow dung and the sheep dung are dry dung obtained by conventional sun-curing fermentation, and the specific method adopts a method well known in the field, is not the protection point of the invention, and is not described herein.|[0040] Example 1|[0041] A method for improving the carbon sequestration potential of soil by using an organic fertilizer comprises the following steps:|[0042] 1) preparing an organic fertilizer: uniformly mixing 32 parts of cow dung, 23 parts of sheep dung, 70 parts of plant straws, 17 parts of plant ash, 13 parts of bean cakes, 1 part of bacillus thuringiensis and 0.2 part of nocardia, and then carrying out aerobic fermentation at the temperature of lower than 60 ℃ until the temperature is not increased any more to obtain an organic fertilizer;|[0043] 2) ridging in a soil carbon sequestration area, wherein the height of each ridge is 10-25cm, the bottom width is 55-65cm, and the ridge interval is 50-60 cm;|[0044] 3) burying straw biochar into furrows during ridging, then applying organic fertilizer, and planting vetch, alfalfa, tamarix chinensis, sesbania and Chinese silvergrass in the last 3-4 months;|[0045] 4) harvesting after the green manure crops are mature, crushing the straws, mixing the crushed straws with organic fertilizers according to the proportion of 1:5, flatly spraying the mixture on the ground until the thickness is 5-10cm, deeply turning the soil for 20-50cm, planting corns in the middle and late April, and carrying out conventional field management.|[0046] Example 2|[0047] A method for improving the carbon sequestration potential of soil by using organic fertilizer is different from the method in the embodiment 1:|[0048] the organic fertilizer in the step 1) comprises the following raw materials in parts by weight:|[0049] 20 parts of cow dung, 12 parts of sheep dung, 63 parts of plant straws, 15 parts of plant ash, 10 parts of bean cakes, 0.75 part of bacillus thuringiensis and 0.25 part of nocardia.|[0050] Example 3|[0051] A method for improving the carbon sequestration potential of soil by using an organic fertilizer is different from that in the embodiment 1:|[0052] the organic fertilizer in the step 1) comprises the following raw materials in parts by weight:|[0053] 45 parts of cow dung, 17 parts of sheep dung, 67 parts of plant straws, 18 parts of plant ash, 11 parts of bean cakes, 1.75 parts of bacillus thuringiensis and 0.25 part of nocardia.|[0054] Example 4|[0055] A method for improving the carbon sequestration potential of soil by using organic fertilizer is different from the method in the embodiment 1:|[0056] the organic fertilizer in the step 1) comprises the following raw materials in parts by weight:|[0057] 55 parts of cow dung, 33 parts of sheep dung, 80 parts of plant straws, 20 parts of plant ash, 15 parts of bean cakes, 1.75 parts of bacillus thuringiensis and 0.25 part of nocardia.|[0058] Comparative example 1|[0059] A soil treatment method, different from example 1:|[0060] the organic fertilizer is replaced by urea and nitrogen-phosphorus-potassium compound fertilizer.|[0061] Comparative example 2|[0062] A soil treatment method, different from example 1:|[0063] biochar is not added in the step 3).|[0064] Comparative example 3|[0065] A soil treatment method, different from example 1:|[0066] no green manure crop is planted in the step 3), and the step 4) does not include a step of applying organic fertilizer.|[0067] Technical effects|[0068] The first year corn yield and soil carbon fixation after harvesting of the planted corn in examples 1-4 and comparative example 1 are shown in table 1:|[0069] amount of solid carbon (t. hm) -2 ·a -1 )Yield (kg 667 m) -2 )Example 17.53859Example 27.16837Example 37.22841Example 47.45828Comparative example 13.05630Comparative example 25.63723Comparative example 34.11715 |[0070] According to the embodiments, experiments prove that the organic fertilizer is matched with the biochar and the green manure crops for utilization, so that the soil is used for carbon fixationThe amount reaches 7.16-7.53 t.hm -2 ·a -1 Is obviously higher than that of comparative examples 1-3; and the yield of the corn reaches 828-859 kg/mu. Therefore, the method provided by the invention can effectively improve the carbon sequestration potential of the soil and obviously provide the crop yield.|[0071] The above-described embodiments are merely illustrative of the preferred embodiments of the present invention, and do not limit the scope of the present invention, and various modifications and improvements of the technical solutions of the present invention can be made by those skilled in the art without departing from the spirit of the present invention, and the technical solutions of the present invention are within the scope of the present invention defined by the claims. (CN114982414)|TECHNICAL FIELD|[0001] The invention relates to the field of soil improvement, in particular to a method for improving the carbon sequestration potential of soil by using an organic fertilizer.|BACKGROUND ART|[0002] The soil carbon sink is an important path for reducing carbon emission and relieving global climate change. In the global carbon cycle, the soil carbon reservoir is 5 times as large as that of forests and other vegetation, and 3 times as large as that of atmospheric air. 60% of carbon in the soil carbon reservoir exists in soil in the form of organic matters, and the huge soil carbon storage amount is CO in the atmosphere 2 The level of (c) has a significant effect.|[0003] However, the basic national situation of China is that many people have less land, and the rapid urbanization process causes a great reduction in the cultivated land and faces the dilemma of cultivated land loss and quality reduction. The newly reclaimed farmland generally has the problem of low soil fertility, 80 percent of original organic carbon of surface soil is mineralized and decomposed in the soil disturbance process, and the organic carbon reserve of the soil is extremely low and is only 40-60 percent of that of a normal farmland.|[0004] Therefore, how to provide a method capable of effectively improving the carbon sequestration potential of soil is a technical problem which needs to be solved urgently by the technical personnel in the field.|DISCLOSURE|Disclosure of Invention|[0005] The invention aims to provide a method for improving the carbon sequestration potential of soil by utilizing an organic fertilizer, so as to solve the problems in the prior art.|[0006] In order to achieve the purpose, the invention provides the following scheme:|[0007] a method for improving the carbon sequestration potential of soil by using an organic fertilizer comprises the following steps:|[0008] 1) ridging a soil carbon sequestration area, burying biochar into furrows, applying an organic fertilizer, and planting green manure crops;|[0009] 2) after the green manure crops are harvested, the straws are crushed, mixed with organic fertilizer and then spread on the ground, and the soil is turned deeply, so that the crops can be planted.|[0010] Preferably, the organic fertilizer in the steps 1) and 2) comprises the following raw materials in parts by weight:|[0011] 20-55 parts of cow dung, 10-35 parts of sheep dung, 60-80 parts of plant straws, 15-20 parts of plant ash, 10-15 parts of bean cakes and 1-2 parts of microbial bacteria.|[0012] Preferably, the microorganism bacteria comprise bacillus thuringiensis and nocardia, and the ratio of the inoculation amount of the bacillus thuringiensis to the inoculation amount of the nocardia is (3-7): 1.|[0013] Preferably, the application amount of the organic fertilizer in the step 1) is 65-80kg per mu.|[0014] Preferably, the ridge height of the ridges in the step 1) is 10-25cm, the bottom width is 55-65cm, and the ridge distance is 50-60 cm.|[0015] Preferably, the biochar in the step 1) is prepared by taking straws as raw materials; the green manure crops comprise one or more of vetch, alfalfa, tamarisk, sesbania and miscanthus.|[0016] Preferably, the mixing ratio of the straws and the organic fertilizer in the step 2) is 1 (5-7).|[0017] Preferably, the thickness of the flat sprinkling in the step 2) is 5-10 cm; the deep ploughing depth is 20-50 cm.|[0018] Preferably, the method further comprises the following steps:|[0019] 3) after harvesting the crops in the previous season every year, flatly spraying organic fertilizer on the ground surface, deeply turning to soil, and then planting the crops in the next season.|[0020] Preferably, the thickness of the flat-sprinkling organic fertilizer in the step 3) is 8-13 cm; the deep ploughing depth is 20-50 cm.|[0021] The invention discloses a method for improving soil carbon sequestration potential by using an organic fertilizer, which improves the soil structure, increases the carbon sequestration surface area of soil aggregates, increases fertility, loosens the soil, improves the soil permeability, is beneficial to the update of crop roots and improves the carbon sequestration capacity of the soil. The simple substance carbon in the charcoal powder used in the invention can be fixed in the soil basically and irreversibly, thus increasing the carbon sink of the soil, and moreover, the charcoal has fluffy characteristic, so that the porosity structure of the soil can be increased rapidly, and the ventilation effect of the soil is improved. In addition, the green manure crops planted in the invention can provide fertilizer sources for crops and improve soil fertility, and after the straws and the organic fertilizer are deeply turned into the soil, the microorganisms in the organic fertilizer can promote the straws to be thoroughly decomposed, so that soil organic matters are further improved, the carbon sequestration capacity of the soil is improved, and the growth of the crops is facilitated.|INVENTION MODE|Detailed Description|[0022] The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.|[0023] The present invention will be described in further detail with reference to specific embodiments in order to make the above objects, features and advantages more apparent and understandable.|[0024] A method for improving the carbon sequestration potential of soil by using an organic fertilizer comprises the following steps:|[0025] 1) ridging in a soil carbon sequestration area, then burying biochar into furrows, applying an organic fertilizer, and then planting green manure crops;|[0026] 2) after the green manure crops are harvested, the straws are crushed, mixed with organic fertilizer and then spread on the ground, and the soil is turned deeply, so that the crops can be planted.|[0027] In some embodiments of the present invention, the organic fertilizer in steps 1) and 2) comprises the following raw materials in parts by weight:|[0028] 20-55 parts of cow dung, 10-35 parts of sheep dung, 60-80 parts of plant straws, 15-20 parts of plant ash, 10-15 parts of bean cakes and 1-2 parts of microbial bacteria. The conventional organic fertilizer has certain effect on improving the carbon sequestration potential of soil, but the further improvement is not easy on the basis, and the inventor finds that the improvement effect of different types of organic fertilizers on the carbon sequestration potential of soil is far from each other through experimental research, the different kinds of organic fertilizers are compounded in different proportions, so that the effect of improving the carbon fixation effect of the soil is far from each other, therefore, the invention creatively selects 20-55 parts of cow dung, 10-35 parts of sheep dung, 60-80 parts of plant straws, 15-20 parts of plant ash, 10-15 parts of bean cakes and 1-2 parts of microbial bacteria to form the compound organic fertilizer, when used alone, the organic fertilizer has no obvious difference with the conventional organic fertilizer of the same type in improving the soil carbon fixation effect, but when the fertilizer is used together with biochar and green manure crops, the soil carbon sequestration effect is obviously improved.|[0029] In some embodiments of the invention, the microorganism comprises bacillus thuringiensis and nocardia, and the ratio of the inoculum size of bacillus thuringiensis to nocardia is (3-7): 1.|[0030] The present invention is not particularly limited in the source of the bacterial species, and the bacterial species may be isolated by itself or purchased directly, and the technical effects of the present invention can be achieved as long as the ratio of the bacterial species to the inoculum size of Bacillus thuringiensis and Nocardia is (3-7): 1. In some embodiments of the invention, it is preferred to purchase Bacillus thuringiensis and Nocardia directly.|[0031] In some embodiments of the invention, the application amount of the organic fertilizer in the step 1) is 65-80kg per mu.|[0032] In some embodiments of the invention, the ridges in step 1) have a ridge height of 10-25cm, a bottom width of 55-65cm, and a ridge spacing of 50-60 cm.|[0033] If not specifically stated, the present invention does not specifically limit the type of the biochar, and optionally, the biochar is prepared from crop straws or forest, wood and grass, and in some embodiments of the present invention, the biochar in step 1) is prepared from straws as a raw material; the green manure crops comprise one or more of vetch, alfalfa, tamarisk, sesbania and miscanthus.|[0034] In some embodiments of the invention, the mixing ratio of the straws and the organic fertilizer in the step 2) is 1 (5-7).|[0035] If not specifically stated, the thickness of the flat sprinkling fertilizer is not particularly limited by the invention, and the conventional application amount of the organic fertilizer is met, and in some embodiments of the invention, the thickness of the flat sprinkling fertilizer in the step 2) is 5-10 cm; the depth of the deep ploughing is not particularly limited as long as the conventional application mode of the organic fertilizer is satisfied, and in some embodiments, the depth of the deep ploughing is preferably 20-50 cm.|[0036] In some embodiments of the invention, the method for improving the carbon sequestration potential of soil by using the organic fertilizer further comprises the following steps:|[0037] 3) after harvesting the crops of the previous season every year, organic fertilizer is horizontally sprayed on the ground surface and deeply ploughed to soil, and then the crops of the next season are planted.|[0038] The thickness of the flat spraying fertilizer is not particularly limited if not specifically stated, and the conventional application amount of the organic fertilizer is met, and in some embodiments of the invention, the thickness of the flat spraying organic fertilizer in the step 3) is 8-13 cm; the present invention has no particular limitation on the depth of the deep ploughing, unless otherwise specified, as long as the conventional application manner of the organic fertilizer is satisfied, and in some embodiments of the present invention, the depth of the deep ploughing in step 3) is preferably 20 to 50 cm.|[0039] The technical solution of the present invention will be described in detail below with reference to specific examples. The straw biochar in the following examples is biochar obtained by calcining corn straws. The specific preparation method is conventional technology, and is not described herein. The cow dung and the sheep dung are dry dung obtained by conventional sun-curing fermentation, and the specific method adopts a method well known in the field, is not the protection point of the invention, and is not described herein.|[0040] Example 1|[0041] A method for improving the carbon sequestration potential of soil by using an organic fertilizer comprises the following steps:|[0042] 1) preparing an organic fertilizer: uniformly mixing 32 parts of cow dung, 23 parts of sheep dung, 70 parts of plant straws, 17 parts of plant ash, 13 parts of bean cakes, 1 part of bacillus thuringiensis and 0.2 part of nocardia, and then carrying out aerobic fermentation at the temperature of lower than 60 ℃ until the temperature is not increased any more to obtain an organic fertilizer;|[0043] 2) ridging in a soil carbon sequestration area, wherein the height of each ridge is 10-25cm, the bottom width is 55-65cm, and the ridge interval is 50-60 cm;|[0044] 3) burying straw biochar into furrows during ridging, then applying organic fertilizer, and planting vetch, alfalfa, tamarix chinensis, sesbania and Chinese silvergrass in the last 3-4 months;|[0045] 4) harvesting after the green manure crops are mature, crushing the straws, mixing the crushed straws with organic fertilizers according to the proportion of 1:5, flatly spraying the mixture on the ground until the thickness is 5-10cm, deeply turning the soil for 20-50cm, planting corns in the middle and late April, and carrying out conventional field management.|[0046] Example 2|[0047] A method for improving the carbon sequestration potential of soil by using organic fertilizer is different from the method in the embodiment 1:|[0048] the organic fertilizer in the step 1) comprises the following raw materials in parts by weight:|[0049] 20 parts of cow dung, 12 parts of sheep dung, 63 parts of plant straws, 15 parts of plant ash, 10 parts of bean cakes, 0.75 part of bacillus thuringiensis and 0.25 part of nocardia.|[0050] Example 3|[0051] A method for improving the carbon sequestration potential of soil by using an organic fertilizer is different from that in the embodiment 1:|[0052] the organic fertilizer in the step 1) comprises the following raw materials in parts by weight:|[0053] 45 parts of cow dung, 17 parts of sheep dung, 67 parts of plant straws, 18 parts of plant ash, 11 parts of bean cakes, 1.75 parts of bacillus thuringiensis and 0.25 part of nocardia.|[0054] Example 4|[0055] A method for improving the carbon sequestration potential of soil by using organic fertilizer is different from the method in the embodiment 1:|[0056] the organic fertilizer in the step 1) comprises the following raw materials in parts by weight:|[0057] 55 parts of cow dung, 33 parts of sheep dung, 80 parts of plant straws, 20 parts of plant ash, 15 parts of bean cakes, 1.75 parts of bacillus thuringiensis and 0.25 part of nocardia.|[0058] Comparative example 1|[0059] A soil treatment method, different from example 1:|[0060] the organic fertilizer is replaced by urea and nitrogen-phosphorus-potassium compound fertilizer.|[0061] Comparative example 2|[0062] A soil treatment method, different from example 1:|[0063] biochar is not added in the step 3).|[0064] Comparative example 3|[0065] A soil treatment method, different from example 1:|[0066] no green manure crop is planted in the step 3), and the step 4) does not include a step of applying organic fertilizer.|[0067] Technical effects|[0068] The first year corn yield and soil carbon fixation after harvesting of the planted corn in examples 1-4 and comparative example 1 are shown in table 1:|[0069] amount of solid carbon (t. hm) -2 ·a -1 )Yield (kg 667 m) -2 )Example 17.53859Example 27.16837Example 37.22841Example 47.45828Comparative example 13.05630Comparative example 25.63723Comparative example 34.11715 |[0070] According to the embodiments, experiments prove that the organic fertilizer is matched with the biochar and the green manure crops for utilization, so that the soil is used for carbon fixationThe amount reaches 7.16-7.53 t.hm -2 ·a -1 Is obviously higher than that of comparative examples 1-3; and the yield of the corn reaches 828-859 kg/mu. Therefore, the method provided by the invention can effectively improve the carbon sequestration potential of the soil and obviously provide the crop yield.|[0071] The above-described embodiments are merely illustrative of the preferred embodiments of the present invention, and do not limit the scope of the present invention, and various modifications and improvements of the technical solutions of the present invention can be made by those skilled in the art without departing from the spirit of the present invention, and the technical solutions of the present invention are within the scope of the present invention defined by the claims. Family Number|(101616186)|101616186|Abstract|(CN114982414 A)|The invention discloses a method for improving the carbon sequestration potential of soil by using an organic fertilizer , and belongs to the technical field of soil improvement , and the method specifically comprises the following steps : 1 ) ridging in a soil carbon sequestration area , then burying biochar into furrows , then applying the organic fertilizer , and then planting green manure crops ; and ( 2 ) after the green manure crops are harvested , crushing straws of the green manure crops , mixing the crushed straws with an organic fertilizer , flatly spraying the mixture on the ground , and deeply ploughing the soil , so that the crops can be planted . The organic fertilizer is matched with the biochar and green manure crops for use , the surface area of soil aggregate carbon sequestration is increased , the carbon sequestration capacity of soil is improved , meanwhile , the soil fertility and air permeability are improved , growth of crops is facilitated , and the yield of the crops can be remarkably increased . |CPC codes|(CN114982414 A)|A01B - 079/02 |A01C - 021/00 |IPC codes|(CN114982414 A)|A01B - 079/02 |A01C - 021/00 |Title|(CN114982414 A)|Method for improving carbon sequestration potential of soil by using organic fertilizer | Basic materials chemistry|Other special machines A01B-079/02|A01C-021/00|C05D-001/00|C05F-017/20|C05F-017/50|C05G-003/80|Y02W-030/40 (GR1) C05D-001/00[RK1]; C05F-003/00[RK2]; C05F-005/00/2[RK3]; C05F-011/00[RK4]; C05F-011/08[RK5]; C05F-017/20[RK6]; C05F-017/50[RK7]; C05G-003/80[RK8] A01B-079/02|A01C-021/00|C05D-001/00|C05F-017/20|C05F-017/50|C05G-003/80|Y02W-030/40 A01B-079/02|A01C-021/00|C05F-017/20|C05F-017/50|C05G-003/80 A01B-079/02|A01C-021/00|C05F-017/20|C05F-017/50|C05G-003/80 CN117296507|CN116806477|CN118715963|CN116584327B|TWI822643 CN117296507 107984827 WHO=Examiner SELF=N CAT=Y|CN116806477 106681485 WHO=Examiner SELF=N CAT=Y|CN118715963 111660119 WHO=Examiner SELF=N CAT=A|CN116584327B 106131242 WHO=Examiner SELF=N|TWI822643 108270788 WHO=Examiner SELF=N CN104641756|US20210032538|CN107509406|CN106576486|CN105175180 CN104641756 69443585 WHO=Examiner SELF=N CAT=X|US20210032538 86298743 WHO=Examiner SELF=N CAT=A|CN107509406 78181621 WHO=Examiner SELF=N CAT=A|CN106576486 75977776 WHO=Examiner SELF=N CAT=A|CN105175180 71810448 WHO=Examiner SELF=N CAT=A CN104641756; CN105175180; CN106576486; CN107509406; US20210032538 REVOKED (CN114982414)|REVOKED DEAD (CN114982414)|DEAD (CN114982414)|LEGAL DETAILS FOR CN114982414|Actual or expected expiration date=2024-03-01|Legal state=DEAD|Status=REVOKED|Event publication date=2022-06-22|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210712347|Application date=2022-06-22|Standardized application number=2022CN-0712347|Event publication date=2022-09-02|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114982414|Publication stage code=A|Publication date=2022-09-02|Standardized publication number=CN114982414|Event publication date=2022-09-02|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-09-20|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-03-01|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTt3cR4Q6cWIVfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=JlkXmkfbd33h%252FsMuf%252F6bGZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN114982414)|CN (CN114982414)|NAME=LIAONING AGRICULTURAL DEV SERVICE CENTER , COUNTRY=CN (CN114982414)|NAME=CHEN YUEXIA;BEIJING ORIENTAL SHENGFAN INTELLECTUAL PROPERTY AGENCY FIRM , REG=11562 (CN114982414)|CN (CN114982414)|NAME=SONG DAN, COUNTRY=CN |NAME=WANG JILEI 0 1 Titre: (CN114982414)|Method for improving carbon sequestration potential of soil by using organic fertilizer Résumé: (CN114982414)|The invention discloses a method for improving the carbon sequestration potential of soil by using an organic fertilizer, and belongs to the technical field of soil improvement, and the method specifically comprises the following steps: 1) ridging in a soil carbon sequestration area, then burying biochar into furrows, then applying the organic fertilizer, and then planting green manure crops; and (2) after the green manure crops are harvested, crushing straws of the green manure crops, mixing the crushed straws with an organic fertilizer, flatly spraying the mixture on the ground, and deeply ploughing the soil, so that the crops can be planted. The organic fertilizer is matched with the biochar and green manure crops for use, the surface area of soil aggregate carbon sequestration is increased, the carbon sequestration capacity of soil is improved, meanwhile, the soil fertility and air permeability are improved, growth of crops is facilitated, and the yield of the crops can be remarkably increased. 55 Abstract gpt-4o-mini no The article focuses on improving soil carbon sequestration using organic fertilizers and biochar, without addressing the accelerated weathering of minerals or CO₂ capture through mineral carbonation.
56 CN202310772359 CN202310772359 CN116784039 106614910 CN116784039 A 2023-09-22 [CN116784039] 2023-06-28 2023-06-28 2023-09-22 (CN116784039)|2026-03-20 (CN116784039)|Method for rapidly increasing soil organic carbon in Jianghuai rice field based on straw decay promotion and returning (CN116784039)|The invention provides a method for rapidly increasing soil organic carbon of a rice field in Jianghuai province based on straw decay promotion and returning, and relates to the field of straw returning, and the method comprises the following operation steps: straw crushing, base fertilizer application and C/N ratio regulation and control, straw decay agent selection and application, shallow rotation and irrigation, rice seedling transplanting, topdressing and soil carbon sequestration efficiency excitation. The ratio of N to P2O5 to K2O in the organic-inorganic compound fertilizer in the step S1 is 17%: 15%: 8%, and the organic-inorganic compound fertilizer contains organic matters gt; according to the method for rapidly increasing the soil organic carbon of the Jianghuai rice field based on straw decay promotion and field returning, the soil improvement effect is remarkable, the organic matter mutability of soil of a plough layer can be improved, meanwhile, the soil organic carbon storage amount is effectively increased, and the good carbon sequestration effect is achieved; according to the method for rapidly increasing the soil organic carbon of the Jianghuai rice field based on straw decay promoting and returning, the procedure is simple, operation is convenient, common farmers can complete the method, and large-scale popularization of the technology is facilitated. ANHUI AGRICULTURAL UNIVERSITY (CN116784039)|ANHUI AGRICULTURAL UNIVERSITY ([CN]) MA CHAO|SHI XINYI|WU ZELU|LU MENGXING|TANG YUEYUE|GUO MENGMENG|LIU ZIXIN|WEI ZHENGYU|ZHU LIN (CN116784039)|MA CHAO|SHI XINYI|WU ZELU|LU MENGXING|TANG YUEYUE|GUO MENGMENG|LIU ZIXIN|WEI ZHENGYU|ZHU LIN (CN116784039)|WU QI;Hefei Lawong Patent Agency (General Partnership)|Reg. Nb: 34140 (CN116784039)|However, the stalk rot is difficult to exert and stably obtain ideal results due to the effect of the stalk rot caused by various factors such as decomposition mode, regional climate, soil characteristics, antagonism/synergistic effect of indigenous microorganisms and the like.| (CN116784039)|1. A method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized by comprising the following steps: the method comprises the following operation steps:s1, crushing straw: harvesting by using a combine harvester with a cutting device, so that the length of the chopped straw is less than 10cm, and the height of the stubble is less than 10cm;s2, base fertilizer application and C/N ratio regulation: applying fertilizers according to a proposal of local soil testing formula fertilization, and selecting two fertilizers of organic and inorganic compound fertilizers and urea, wherein the nitrogen consumption of the base fertilizer is required to be adjusted by combining the C/N ratio and the consumption of the straws, so that the initial C/N ratio of the returned straws is (16-20): 1;s3, selecting and applying a stalk rot agent: selecting a stalk rot agent which can keep higher activity under the conditions of high temperature of 25-35 ℃ and pH of 5.0-7.5 and intermittent flooding, and uniformly spraying the stalk rot agent on the returning stalks after activating and diluting according to the dosage of 2kg per mu;s4, shallow rotation and irrigation: shallow-rotating the straw, organic and inorganic compound fertilizer, urea, stalk rot and the like on the field into soil by using a rotary cultivator, wherein the rotary cultivation depth is controlled to be 5-15cm; then irrigation is carried out, a thin water layer with the thickness of 5-25mm is reserved on the field surface in the green-returning period, the volume water content of the rice field is used as an irrigation regulation index, and the water layer is not established on the field surface after irrigation;s5, transplanting rice seedlings, topdressing and soil carbon fixation efficiency excitation: transplanting rice seedlings after irrigation is finished, applying a residual nitrogen fertilizer by dressing a base fertilizer in a tillering stage of the rice, and simultaneously applying FeSO (FeSO) according to 5-10 kg/mu in a region with an effective iron background value of soil lower than 10mg/kg 4 ·H 2 O。|2. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: organic-inorganic compound fertilizer N in step S1: p (P) 2 O 5 :K 2 The O ratio is 17%:15%:8% of organic matters of the organic-inorganic compound fertilizer>10%。|3. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: the stalk rot agent functional microorganism in the step S3 is mainly fungi.|4. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: the stalk agent in the step S3 is activated and diluted according to the following formula 1:100 was dissolved in water and incubated at 30℃for 24 hours.|5. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: the iron fertilizer in the step S5 is ferrous sulfate, and the specific dosage is combined with the effective iron content (lower than 10 mg/kg) of the local soil, and FeSO is generally required to be applied 4 ·H 2 O7 kg/mu.|6. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: the stalk agent spraying device in the step S3 is an agent spraying device, the agent spraying device and the rotary cultivator in the step S4 are of an integrated structure, the rotary cultivator comprises rotary tillage mechanisms (1), material containing pieces (4) arranged on two sides of the top end of each rotary tillage mechanism (1), one ends of the two material containing pieces (4) are respectively provided with a transmission piece (3) connected with each rotary tillage mechanism (1), the bottom ends of the two material containing pieces (4) are respectively provided with a spraying pipe (2) extending to one side, the side surfaces of the two material containing pieces (4) are respectively provided with a pressing piece (6), and one end of each pressing piece (6) is provided with a linkage piece (5) connected with each transmission piece (3);the rotary tillage machine is characterized in that the material containing piece (4) comprises a material barrel (41) fixed at the top end of the rotary tillage mechanism (1), a connecting shaft (42) penetrating through the material barrel (41) and connected with the transmission piece (3) is rotatably arranged in the middle of the material barrel (41), and a plurality of stirring blades (43) are sleeved on the outer side of the connecting shaft (42) and the inner side of the material barrel (41).|7. The method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized by comprising the following steps of: the pressurizing piece (6) comprises a shell (61) fixed on the side face of the material containing piece (4), a screw rod (63) penetrating through the shell (61) and connected with the linkage piece (5) is rotationally arranged in the middle of the shell (61), a piston (62) connected with the shell (61) is sleeved on the outer side of the screw rod (63) and located on the inner side of the shell (61), an air inlet valve (65) is arranged at one end of the shell (61), and an air outlet valve (64) connected with the material cylinder (41) is arranged at one side of the air inlet valve (65).|8. The method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized by comprising the following steps of: the spraying pipe (2) comprises a hose (21) with a spray head, a valve (22) arranged in the middle of the hose (21), and a support rod (23) arranged at one end of the hose (21) and above the spray head of the hose (21).|9. The method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized by comprising the following steps of: both sides of the stirring blade (43) are provided with baffle plates which are arranged at equal angles, and the edge of the stirring blade (43) is provided with a plurality of shearing teeth.|10. The method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized in that: the screw rod (63) is a reciprocating screw rod.| (CN116784039)|The invention aims to provide a method for rapidly improving organic carbon in soil of a Jianghuai paddy field based on straw decay promotion and returning to the field, so as to solve the technical problem that the influence of straw decay agent under straw returning to the field on the carbon fixation effect of soil is still unknown.|The invention provides a method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw corrosion promotion and returning to the field, which relates to strawThe field of returning stalks to fields comprises the following operation steps: straw crushing, base fertilizer application, C/N ratio regulation and control, straw-rotting agent selection and application, shallow rotation and irrigation, transplanting, topdressing and soil carbon fixation efficiency excitation, and an organic-inorganic compound fertilizer N in the step S1: p (P) 2 O 5 :K 2 The O ratio is 17%:15%:8% of organic matters of the organic-inorganic compound fertilizer>10% of the invention provides a method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw corrosion promotion and returning to fields, which has remarkable soil improvement effect, can realize the improvement of the organic matter variability of soil in cultivated layers, effectively improves the organic carbon reserves of soil and has good carbon fixation effect. The invention relates to the field of straw returning, in particular to a method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw corrosion promotion and returning.| (CN116784039)|STRAW(100,42)|ORGANIC CARBON(100,25)|JIANGHUAI PADDY FIELD(100,20)|JIANGHUAI PADDY FIELD SOIL(100,20)|PROMOTION(100,14)|RICE TRANSPLANTING SEEDLING(99,6)|STRAW CORROSION PROMOTION(91,7)|STALK ROT(81,12)|ROTARY TILLAGE(78,13)|STRAW DECAY INFLUENCE(61,1)|INDIGENOUS MICROORGANISM(57,1)|INORGANIC COMPOUND FERTILIZER(54,21)|STIRRING BLADE(53,8)|RETURNING STALK(52,4)|RICE TILLERING(52,3)|CLIMATE REGION(49,1)|IRRIGATION REGULATION INDEX(48,3)|CHOPPED STRAW(48,2)|STRAW DECAY(48,1)|STRAW CRUSHING(47,1)|SHEARING TOOTH(43,3)|PIECE PRESSURIZATION(43,1)|SPRAY PIPE(42,5)|INTERMITTENT FLOODING(42,3)|IRRIGATION(40,22)|STRAW CONSUMPTION(40,3)|ROTARY TILLAGE MACHINE(40,2)|CRUSHING STRAW(39,3)|STALK(38,17)|EXCITING EFFICIENCY(38,4)|BASE FERTILIZER(37,18)|SLIDING SOIL CARBON FIXATION(37,4)|ROTARY CULTIVATION DEPTH(37,3)|SOIL TESTING FORMULA FERTILIZATION(37,2)|STRAW ROTTING AGENT SELECTION(37,1)|LINKAGE PIECE(36,5)|SHELL(35,7)|TRANSMISSION PIECE(34,8)|RECIPROCATING SCREW ROD(34,2)|SCREW ROD(33,10)|RETURNED STRAW(33,3)|STUBBLE HEIGHT(33,3)|ROTARY CULTIVATOR(32,9)|SOIL CARBON FIXATION(32,5)|IRON FERTILIZER(32,4)|AGENT FUNCTIONAL MICROORGANISM(32,3)|SOIL ORGANIC MATTER VARIABILITY(32,1)|PRESSING PIECE(31,6)|GROUND(28,19)|SHALLOW ROTATION(28,7)|DOSAGE(27,5)|SLIDING DILUTING(27,3)|ROT SLIDING(27,2)|BASE FERTILIZER NITROGEN CONSUMPTION(26,3)|FERTILIZER APPLICATION(26,3)|NITROGEN CONSUMPTION(26,3)|ANTAGONISM SYNERGISTIC(26,1)|DECOMPOSITION MODE(25,1)|TRANSPLANT(25,1)|SLIDING FESO(24,5)|RESIDUAL NITROGEN FERTILIZER(24,4)|APPLYING FESO(24,3)|IRON CONTENT(24,3)|MATERIAL BARREL(23,12)|INORGANIC COMPOUND(22,21)|RETURNING STALK STRAWTHE FIELD(22,1)|AGENT SELECTION(21,1)|HOSE(20,7)|SPRAY HEAD(20,3)|CULTIVATED LAYER(20,2)|COMBINE HARVESTER(18,3)|ORGANIC MATTER VARIABILITY(18,2)|TOP DRESSING(17,6)|FERROUS SULFATE(17,2)|UREA(16,10)|CARBON FIXATION(16,4)|FUNGUS(15,3)|PADDY RICE SEED(15,3)|STILL UNKNOWN(15,1)|SLIDING APPLYING(14,4)|GREEN RETURNING PERIOD(14,3)|MATERIAL BARREL MIDDLE(14,3)|TILLERING FERTILIZER(14,3)|RICE STUBBLE STRAW DECAY(14,1)|FORMULATED FERTILIZATION SLIDING STRAW(13,2)|MATERIAL CYLINDER(13,1)|AIR INLET VALVE(12,8)|SOIL IMPROVEMENT(12,2)|FERTILIZING SOIL TESTING(11,4)|GRAMINEOUS CROP STRAW(11,1)|LIGNOCELLULOSE DEGRADATION(11,1)|STRAW FIELD(11,1)|STRAWTHE FIELD(11,1)|ORGANIC MATTER(10,8)|NITROGEN FERTILIZER SLIDING FESO(10,3)|BAFFLE PLATE(10,2)|EQUAL ANGLE(10,2)|MASSIVE INCINERATION SLIDING PILING(10,1)|SLIDING CONTROL(10,1)|STRUCTURE INTEGRATION(9,3)|WATER THIN LAYER(9,3)|AGRICULTURAL GARDEN(9,2)|LUJIANG COUNTY(9,2)|SLIDING STRAW DECOMPOSITION(9,2)|SOIL TESTING FORMULATED FERTILIZATION(9,2)|PESTICIDE SPRAYING SLIDING WEEDING(9,1)|RECYCLING STRAW RESOURCE(9,1)|WHEAT STRAW DECOMPOSITION(9,1)|WATER LAYER(8,7)|AIR OUTLET VALVE(8,5)|SLIDING DEVICE(8,3)|STRAW CROP(8,2)|CROP STRAW RESOURCE(8,1)|TRANSPLANTING SLIDING TOP DRESSING(7,4)|VOLUME WATER CONTENT(7,3)|SOIL TESTING FERTILIZATION PROPOSAL(7,1)|STRAW ROTARY TILLAGE(7,1)|KG MU(6,6)|SUPPORT ROD(6,4)|SLIDING RETURNING(6,3)|STALK AGENT TREATMENT(6,3)|UREA NITROGEN CONTENT(6,3)|MICROORGANISM FUNCTION(6,2)|NITROGEN FERTILIZER ACCOUNTING(6,2)|RETURNING STRAW(6,2)|ISFERROUS SULFATE(6,1)|MICROBIAL INOCULUM(6,1)|SOIL MEASUREMENT FORMULA FERTILIZATION(6,1)|STRAW ANNUAL YIELD(6,1)|TURNING REGULATION SLIDING IRRIGATION(6,1)|LINKAGE MEMBER(5,3)|O135KG HM(5,3)|PRESSURIZING MEMBER(5,3)|CMPI CONTENT(5,2)|CPI CONTENT(5,2)|TESTING EARTH(5,2)|AGRICULTURE SUSTAINABLE DEVELOPMENT(5,1)|AGRONOMIC MEASURE(5,1)|IRRIGATION REGULATION(5,1)|RICE SOIL(5,1)|ROTARY TILLAGE DEPTH(5,1)|SLIDING PLOWING DEPTH(5,1)|SLIDING ROTARY TILLAGE(5,1)|SLIDING STRAW RETURNING(5,1)|STALK INFLUENCE(5,1)|STRAW DOSAGE(5,1)|STRAW INFLUENCE(5,1)|STRAW PROMOTION(5,1)|SYNERGY SLIDING YIELD(5,1)|OUTER SIDE(4,6)|ORGANIC CARBON CONTENT(4,5)|C N RATIO REGULATION(4,4)|00KG HM(4,2)|BACTERIA(4,2)|FEED CYLINDER(4,2)|JIANGHUAI COASTAL PADDY FIELD(4,2)|LIQUID PHARMACEUTICAL(4,2)|ROTARY TILLAGE ROTATING SHAFT(4,2)|ROTARY TILLAGE TOP END(4,2)|STRAW DEGRADATION(4,2)|CHARGE BARREL(4,1)|CULTIVATED LAYER SOIL(4,1)|HUNDRED MILLION TON(4,1)|MOISTURE MANAGEMENT(4,1)|NITROGEN FERTILIZER DOSAGE(4,1)|RECIPROCATING SCREW(4,1)|SCREW ROD PENETRATION(4,1)|SHALLOW ROTARY DEPTH(4,1)|STRAW DECOMPOSING AGENT DISTRIBUTION(4,1)|UNBALANCED NUTRIENT INPUT(4,1)|TEST MODE(3,4)|IRON BACKGROUND(3,3)|SLIDING ORGANIC MATTER(3,3)|ADVANCED WATER SAVING IRRIGATION(3,1)|AGRICULTURAL SCIENTIST(3,1)|CARBON LIBRARY CHANGE TREND(3,1)|EARTH COMPONENT(3,1)|EQUIANGULAR ARRANGEMENT(3,1)|FARMLAND SLIDING EMISSION REDUCTION(3,1)|INSIGNIFICANT DIFFERENCE(3,1)|JIANGHUAI REGION(3,1)|NITROGEN FERTILIZER CONSUMPTION(3,1)|ROTARY TILLAGE CONFIGURATION(3,1)|SLIDING SHELL(3,1)|SOIL FERTILITY TEST(3,1)|SOIL LAYER SOC CONTENT(3,1)|SOIL MAIN NUTRIENT CONTENT(3,1)|STALK ROTTING(3,1)|STATE CARBON BALANCE(3,1)|STIRRING LEAF(3,1)|STRAW DECOMPOSITION RATE(3,1)|STRAW ROTTING(3,1)|ACTINOMYCETE(2,1)|AGRICULTURAL PRODUCTIVITY(2,1)|ALKALINE HYDROLYSIS NITROGEN CONTENT(2,1)|CRUSHING(2,1)|FERTILITY LEVEL(2,1)|GROUND LAYER(2,1)|GROWER(2,1)| (CN116784039)|1. A method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized by comprising the following steps: the method comprises the following operation steps:|s1, crushing straw: harvesting by using a combine harvester with a cutting device, so that the length of the chopped straw is less than 10cm, and the height of the stubble is less than 10cm;|s2, base fertilizer application and C/N ratio regulation: applying fertilizers according to a proposal of local soil testing formula fertilization, and selecting two fertilizers of organic and inorganic compound fertilizers and urea, wherein the nitrogen consumption of the base fertilizer is required to be adjusted by combining the C/N ratio and the consumption of the straws, so that the initial C/N ratio of the returned straws is (16-20): 1;|s3, selecting and applying a stalk rot agent: selecting a stalk rot agent which can keep higher activity under the conditions of high temperature of 25-35 ℃ and pH of 5.0-7.5 and intermittent flooding, and uniformly spraying the stalk rot agent on the returning stalks after activating and diluting according to the dosage of 2kg per mu;|s4, shallow rotation and irrigation: shallow-rotating the straw, organic and inorganic compound fertilizer, urea, stalk rot and the like on the field into soil by using a rotary cultivator, wherein the rotary cultivation depth is controlled to be 5-15cm; then irrigation is carried out, a thin water layer with the thickness of 5-25mm is reserved on the field surface in the green-returning period, the volume water content of the rice field is used as an irrigation regulation index, and the water layer is not established on the field surface after irrigation;|s5, transplanting rice seedlings, topdressing and soil carbon fixation efficiency excitation: transplanting rice seedlings after irrigation is finished, applying a residual nitrogen fertilizer by dressing a base fertilizer in a tillering stage of the rice, and simultaneously applying FeSO (FeSO) according to 5-10 kg/mu in a region with an effective iron background value of soil lower than 10mg/kg 4 ·H 2 O。|2. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: organic-inorganic compound fertilizer N in step S1: p (P) 2 O 5 :K 2 The O ratio is 17%:15%:8% of organic matters of the organic-inorganic compound fertilizer>10%。|3. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: the stalk rot agent functional microorganism in the step S3 is mainly fungi.|4. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: the stalk agent in the step S3 is activated and diluted according to the following formula 1:100 was dissolved in water and incubated at 30℃for 24 hours.|5. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: the iron fertilizer in the step S5 is ferrous sulfate, and the specific dosage is combined with the effective iron content (lower than 10 mg/kg) of the local soil, and FeSO is generally required to be applied 4 ·H 2 O7 kg/mu.|6. The method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw decay promotion and returning is characterized by comprising the following steps of: the stalk agent spraying device in the step S3 is an agent spraying device, the agent spraying device and the rotary cultivator in the step S4 are of an integrated structure, the rotary cultivator comprises rotary tillage mechanisms (1), material containing pieces (4) arranged on two sides of the top end of each rotary tillage mechanism (1), one ends of the two material containing pieces (4) are respectively provided with a transmission piece (3) connected with each rotary tillage mechanism (1), the bottom ends of the two material containing pieces (4) are respectively provided with a spraying pipe (2) extending to one side, the side surfaces of the two material containing pieces (4) are respectively provided with a pressing piece (6), and one end of each pressing piece (6) is provided with a linkage piece (5) connected with each transmission piece (3);|the rotary tillage machine is characterized in that the material containing piece (4) comprises a material barrel (41) fixed at the top end of the rotary tillage mechanism (1), a connecting shaft (42) penetrating through the material barrel (41) and connected with the transmission piece (3) is rotatably arranged in the middle of the material barrel (41), and a plurality of stirring blades (43) are sleeved on the outer side of the connecting shaft (42) and the inner side of the material barrel (41).|7. The method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized by comprising the following steps of: the pressurizing piece (6) comprises a shell (61) fixed on the side face of the material containing piece (4), a screw rod (63) penetrating through the shell (61) and connected with the linkage piece (5) is rotationally arranged in the middle of the shell (61), a piston (62) connected with the shell (61) is sleeved on the outer side of the screw rod (63) and located on the inner side of the shell (61), an air inlet valve (65) is arranged at one end of the shell (61), and an air outlet valve (64) connected with the material cylinder (41) is arranged at one side of the air inlet valve (65).|8. The method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized by comprising the following steps of: the spraying pipe (2) comprises a hose (21) with a spray head, a valve (22) arranged in the middle of the hose (21), and a support rod (23) arranged at one end of the hose (21) and above the spray head of the hose (21).|9. The method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized by comprising the following steps of: both sides of the stirring blade (43) are provided with baffle plates which are arranged at equal angles, and the edge of the stirring blade (43) is provided with a plurality of shearing teeth.|10. The method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning is characterized in that: the screw rod (63) is a reciprocating screw rod. (CN116784039)|TECHNICAL FIELD|[0001] The invention relates to the field of straw returning, in particular to a method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw corrosion promotion and returning.|BACKGROUND ART|[0002] The straw contains nutrient elements necessary for the growth of crops such as carbon, nitrogen, phosphorus, potassium and the like. The annual yield of straw in China is counted to be more than 10 hundred million tons. In recent years, straw is used as a renewable resource to be returned to the field for use in agricultural production, so that the purposes of fertility improvement, synergy and yield improvement, environmental protection and the like can be realized, and straw returning is an important agronomic measure for recycling straw resources. The organic carbon in the soil is taken as one of important soil components, and has important significance for improving agricultural productivity and realizing land carbon balance. A large number of researches show that the straw returning can obviously improve the organic carbon content of soil, improve the quality of organic carbon and provide important guarantee for improving the carbon fixation and emission reduction of farmlands.|[0003] However, it has also been reported that the straw, especially the straw of gramineous crops, is returned to the field in the current year, and if the returning condition is not properly controlled, the straw which is not thoroughly decomposed can cause adverse effect on the growth of the crops, so that the phenomenon of yield reduction occurs. Therefore, agricultural scientists at home and abroad research on the problems of complex molecular structure, unbalanced C/N ratio, poor single microbial degradation effect and the like of the straws, and point out that the microbial inoculum rich in lignocellulose degrading microorganisms is added in the straw degradation process, so that the straw degradation process in the field in the season can be quickened, the degradation time is shortened, and the adverse effect of direct straw returning to the field on next crop is reduced. However, the stalk rot is difficult to exert and stably obtain ideal results due to the effect of the stalk rot caused by various factors such as decomposition mode, regional climate, soil characteristics, antagonism/synergistic effect of indigenous microorganisms and the like. It is not clear whether the accumulation effect of functional microorganisms in the stalk rot is to the organic matters in the soil of the Jianghuai coastal paddy field after the functional microorganisms are added.|[0004] The paddy fields along the sides of Jianghuai generally have the problems of poor physical properties of soil, weak capacity of regulating and storing water, low fertility level, unbalanced nutrient input, massive incineration and piling of crop straw resources and the like. The former people aim at a large number of soil fertility tests which are carried out on Jianghuai coastal paddy fields. The result shows that the organic carbon content of the soil can be effectively improved by carrying out the straw and chemical fertilizer distribution for a long time, but the influence of the straw returning and the straw-decomposing agent distribution on the carbon fixation effect of the soil is still unclear.|[0005] To sum up, in order to promote the organic carbon content of paddy field soil in Jianghuai region and promote the sustainable development of agriculture in the region, further development and improvement of the technology for promoting the decay of rice stubble straw and returning to the field and fixing carbon are needed.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to provide a method for rapidly improving organic carbon in soil of a Jianghuai paddy field based on straw decay promotion and returning to the field, so as to solve the technical problem that the influence of straw decay agent under straw returning to the field on the carbon fixation effect of soil is still unknown.|[0007] The invention aims to solve the technical problems, and is realized by adopting the following technical scheme:|[0008] a method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning comprises the following operation steps:|[0009] s1, crushing straw: harvesting by using a combine harvester with a cutting device, so that the length of the chopped straw is less than 10cm, and the height of the stubble is less than 10cm;|[0010] s2, base fertilizer application and C/N ratio regulation: applying fertilizers according to a proposal of local soil testing formula fertilization, and selecting two fertilizers of organic and inorganic compound fertilizers and urea, wherein the nitrogen consumption of the base fertilizer is required to be adjusted by combining the C/N ratio and the consumption of the straws, so that the initial C/N ratio of the returned straws is (16-20): 1;|[0011] s3, selecting and applying a stalk rot agent: selecting a stalk rot agent which can keep higher activity under the conditions of high temperature of 25-35 ℃ and pH of 5.0-7.5 and intermittent flooding, and uniformly spraying the stalk rot agent on the returning stalks after activating and diluting according to the dosage of 2kg per mu;|[0012] s4, shallow rotation and irrigation: shallow-rotating the straw, organic and inorganic compound fertilizer, urea, stalk rot and the like on the field into soil by using a rotary cultivator, wherein the rotary cultivation depth is controlled to be 5-15cm; then irrigation is carried out, a thin water layer with the thickness of 5-25mm is reserved on the field surface in the green-returning period, the volume water content of the rice field is used as an irrigation regulation index, and the water layer is not established on the field surface after irrigation;|[0013] s5, transplanting rice seedlings, topdressing and soil carbon fixation efficiency excitation: transplanting rice seedlings after irrigation is finished, applying a residual nitrogen fertilizer by dressing a base fertilizer in a tillering stage of the rice, and simultaneously applying FeSO (FeSO) according to 5-10 kg/mu in a region with an effective iron background value of soil lower than 10mg/kg 4 ·H 2 O。|[0014] Preferably, the organic-inorganic compound fertilizer N in step S1: p (P) 2 O 5 :K 2 The O ratio is 17%:15%:8% of organic matters of the organic-inorganic compound fertilizer>10%。|[0015] Preferably, the stalk rot agent functional microorganism in the step S3 is mainly fungi.|[0016] Preferably, the stalk agent in step S3 is activated and diluted according to 1:100 was dissolved in water and incubated at 30℃for 24 hours.|[0017] Preferably, the iron fertilizer in step S5 isFerrous sulphate is used in a specific amount in combination with the effective iron content of the local soil (less than 10 mg/kg), typically required FeSO to be applied 4 ·H 2 O7 kg/mu.|[0018] Preferably, the stalk agent spraying device in the step S3 is an agent spraying device, the agent spraying device and the rotary cultivator in the step S4 are of an integrated structure, the rotary cultivator comprises a rotary cultivation mechanism, material containing pieces arranged on two sides of the top end of the rotary cultivation mechanism, one ends of the two material containing pieces are respectively provided with a transmission piece connected with the rotary cultivation mechanism, the bottom ends of the two material containing pieces are respectively provided with a spraying pipe extending to one side, the side surfaces of the two material containing pieces are respectively provided with a pressing piece, and one end of the pressing piece is provided with a linkage piece connected with the transmission piece;|[0019] the rotary tillage mechanism comprises a rotary tillage mechanism body, and is characterized in that the material containing piece comprises a material barrel fixed at the top end of the rotary tillage mechanism, a connecting shaft penetrating through the material barrel and connected with the transmission piece is rotationally arranged in the middle of the material barrel, and a plurality of stirring blades are sleeved on the outer side of the connecting shaft and the inner side of the material barrel.|[0020] Preferably, the pressurizing member comprises a shell fixed on the side surface of the material containing member, a screw rod penetrating through the shell and connected with the linkage member is rotationally arranged in the middle of the shell, a piston connected with the shell is sleeved on the outer side of the screw rod and the inner side of the shell, an air inlet valve is arranged at one end of the shell, and an air outlet valve connected with the material barrel is arranged at one end of the shell and positioned at one side of the air inlet valve.|[0021] Preferably, the spraying pipe comprises a hose with a spray head, a valve arranged in the middle of the hose, and a support rod arranged at one end of the hose and above the spray head of the hose.|[0022] Preferably, baffle plates which are arranged at equal angles are arranged on two sides of the stirring blade, and a plurality of shearing teeth are arranged on the edge of the stirring blade.|[0023] Preferably, the screw rod is a reciprocating screw rod.|[0024] The beneficial effects of the invention are as follows:|[0025] 1. the method for rapidly improving organic carbon in soil of the Jianghuai paddy field based on straw corrosion promotion and returning is remarkable in soil improvement effect, capable of improving the variability of organic matters in soil of a cultivated layer, and meanwhile capable of effectively improving the organic carbon reserves of the soil, and good in carbon fixing effect.|[0026] 2. The method for rapidly improving organic carbon in soil of the Jianghuai paddy field based on straw corrosion promotion and returning to the field is simple in procedure, convenient to operate, capable of being completed by general growers, and beneficial to large-scale popularization of the technology.|[0027] 3. According to the rotary tillage machine, spraying and rotary tillage are integrated, the rotary tillage rotating shaft is linked with the screw rod through the transmission piece, the linkage piece and the connecting shaft, when the rotary tillage rotating shaft rotates, the connecting shaft and the screw rod simultaneously rotate, the connecting shaft drives the stirring blade, the stalk rot agent at the inner side of the feed cylinder is mixed with water, the phenomenon of precipitation or layering when liquid medicine moves is avoided, the screw rod drives the piston to reciprocate, the air pressure is supplemented at the inner side of the feed cylinder by matching with the air outlet valve and the air inlet valve, the liquid medicine is prevented from being sprayed by a water pump, the time of spraying rotary tillage is improved, and the straw returning efficiency is improved.|DRAWINGS DESCRIPTION|[0028] FIG. 1 is a schematic diagram showing the effect of different stalk agent treatments on L I content according to the present invention;|[0029] FIG. 2 is a schematic diagram showing the effect of different stalk agent treatments of the present invention on CPI content;|[0030] FIG. 3 is a schematic illustration of the effect of different stalk agent treatments of the present invention on CMPI content;|[0031] FIG. 4 is a schematic diagram showing the effect of different carbon-nitrogen ratio treatments on straw decomposition rate;|[0032] FIG. 5 is a graph showing the effect of different carbon to nitrogen ratio treatments of the present invention on total organic carbon content;|[0033] FIG. 6 is a graph showing the effect of different carbon to nitrogen ratio treatments on L I content according to the present invention;|[0034] FIG. 7 is a graph showing the effect of different carbon to nitrogen ratio treatments of the present invention on CPI content;|[0035] FIG. 8 is a graph showing the effect of different carbon to nitrogen ratio treatments on CMPI content in accordance with the present invention;|[0036] FIG. 9 is a schematic view of the spraying and rotary tillage configuration of the present invention;|[0037] FIG. 10 is a schematic view of a spray tube according to the present invention;|[0038] FIG. 11 is a schematic cross-sectional view of a pod of the present invention;|[0039] FIG. 12 is a schematic cross-sectional view of a compression member of the present invention;|[0040] reference numerals: 1. a rotary tillage mechanism; 2. a spraying tube; 21. a hose; 22. a valve; 23. a support rod; 3. a transmission member; 4. a material containing piece; 41. a charging barrel; 42. a connecting shaft; 43. stirring the leaves; 5. a linkage member; 6. a pressurizing member; 61. a housing; 62. a piston; 63. a screw rod; 64. an air outlet valve; 65. an air inlet valve.|INVENTION MODE|Detailed Description|[0041] In order that the manner in which the above recited features, objects and advantages of the present invention are obtained, a more particular description of the invention will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings. Based on the examples in the embodiments, those skilled in the art can obtain other examples without making any inventive effort, which fall within the scope of the invention.|[0042] Specific embodiments of the present invention are described below with reference to the accompanying drawings.|[0043] Example 1|[0044] A method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning comprises the following operation steps:|[0045] s1, crushing straw: harvesting the straw crops in the regions from the last 5 months to the last 6 months of the year by using a combine harvester with a cutting device after the straw crops in the regions of Jianghuai are ripe, so that the length of the cut straw is less than 10cm and the stubble height is less than 10cm;|[0046] s2, base fertilizer application and C/N ratio regulation: applying fertilizers according to a local soil testing formula fertilization proposal, and selecting two fertilizers of organic and inorganic compound fertilizers and urea, wherein the nitrogen consumption of the base fertilizer is required to be adjusted by combining the C/N ratio and the consumption of the straws, so that the initial C/N ratio of the returned straws is 18:1;|[0047] s3, selecting and applying a stalk rot agent: selecting a stalk rot agent which can keep higher activity under the conditions of high temperature of 25-35 ℃ and pH of 5.0-7.5 and intermittent flooding, and uniformly spraying the stalk rot agent on the returning stalks after activating and diluting according to the dosage of 2kg per mu;|[0048] s4, shallow rotation and irrigation: shallow-rotating the straw, organic and inorganic compound fertilizer, urea, stalk-rotting agent and the like on the field into soil by using a rotary cultivator, wherein the rotary cultivation depth is controlled at 10cm; then irrigation is carried out, a thin water layer with the thickness of 15mm is reserved on the field surface in the green-returning period, the volume water content of the rice field is used as an irrigation regulation index, and the water layer is not established on the field surface after irrigation;|[0049] s5, transplanting rice seedlings, topdressing and soil carbon fixation efficiency excitation: transplanting rice seedlings after irrigation is finished, applying a residual nitrogen fertilizer by dressing a base fertilizer in a tillering stage of the rice, and simultaneously applying FeSO (FeSO) according to 5-10 kg/mu in a region with an effective iron background value of soil lower than 10mg/kg 4 ·H 2 O to promote the soil carbon fixation efficiency.|[0050] Wherein, the organic-inorganic compound fertilizer N in the step S2: p (P) 2 O 5 :K 2 The O ratio is 17%:15%:8% of organic matters of the organic-inorganic compound fertilizer>10%。|[0051] Wherein the stalk rot agent functional microorganism in the step S3 is mainly fungi.|[0052] Wherein, the stalk agent in the step S3 is activated and diluted according to the following formula 1:100 was dissolved in water and incubated at 30℃for 24 hours.|[0053] Wherein the iron fertilizer in the step S5 is ferrous sulfate, the specific dosage is combined with the effective iron content (lower than 10 mg/kg) of the local soil, and FeSO is generally required to be applied 4 ·H 2 O7 kg/mu.|[0054] The stalk agent spraying device in the step S3 is an agent spraying device, the agent spraying device and the rotary cultivator in the step S4 are of an integrated structure, the rotary cultivator comprises a rotary tillage mechanism 1, material containing pieces 4 arranged on two sides of the top end of the rotary tillage mechanism 1, one ends of the two material containing pieces 4 are respectively provided with a transmission piece 3 connected with the rotary tillage mechanism 1, the bottom ends of the two material containing pieces 4 are respectively provided with a spraying pipe 2 extending to one side, the side surfaces of the two material containing pieces 4 are respectively provided with a pressing piece 6, and one end of the pressing piece 6 is provided with a linkage piece 5 connected with the transmission piece 3;|[0055] the material containing piece 4 comprises a material barrel 41 fixed at the top end of the rotary tillage mechanism 1, a connecting shaft 42 penetrating through the material barrel 41 and connected with the transmission piece 3 is rotatably arranged in the middle of the material barrel 41, and a plurality of stirring blades 43 are sleeved on the outer side of the connecting shaft 42 and the inner side of the material barrel 41.|[0056] The pressurizing member 6 includes a housing 61 fixed on the side of the material containing member 4, a screw rod 63 penetrating the housing 61 and connected with the linkage member 5 is rotatably disposed in the middle of the housing 61, a piston 62 connected with the housing 61 is sleeved on the outer side of the screw rod 63 and on the inner side of the housing 61, an air inlet valve 65 is disposed at one end of the housing 61, and an air outlet valve 64 connected with the barrel 41 is disposed at one end of the housing 61 and on one side of the air inlet valve 65.|[0057] Wherein, the spraying pipe 2 comprises a hose 21 with a spray head, a valve 22 arranged in the middle of the hose 21, and a support rod 23 arranged at one end of the hose 21 and above the spray head of the hose 21.|[0058] Wherein, both sides of stirring leaf 43 all are equipped with the baffle that equiangular arrangement, and stirring leaf 43's edge is equipped with a plurality of shearing teeth.|[0059] Wherein the screw 63 is a reciprocating screw.|[0060] As shown in fig. 9-12, in this embodiment, by mounting the material containing member 4 on the rotary tillage mechanism 1 and connecting the material containing member 4 with the rotary tillage mechanism 1 through the transmission member 3, when the rotary tillage mechanism 1 performs rotary tillage, the rotating shaft drives the connecting shaft 42 through the transmission member 3, the connecting shaft 42 drives the stirring blade 43 to rotate at the inner side of the charging barrel 41, the stirring blade 43 mixes the stalk-melting agent at the inner side of the charging barrel 41 with water, and the shearing blade at the edge of the stirring blade 43 improves the uniformity of dispersing the stalk-melting agent in water, simultaneously the transmission member 3 drives the linkage member 5 to operate, the linkage member 5 drives the screw 63 to rotate at the inner side of the housing 61, the piston 62 reciprocates according to the groove on the surface of the screw 63, and simultaneously air between the piston 62 and the housing 61 and the inner side of the pressing charging barrel 41 are pressed through the air outlet valve 64, the inner side of the charging barrel 41 has pressure, and the stalk-melting agent is sprayed through the nozzle of the hose 21 when the valve 22 is opened, so that the stalk-melting efficiency is increased, and the stalk-melting agent needs to be conveyed by the pump.|[0061] The following comparative experiments were carried out on the method for rapidly improving organic carbon in soil of Jianghuai paddy field by promoting straw to decay and returning to field in the present example:|[0062] in this example, F1 is a stalk-forming agent mainly composed of bacteria, F2 is a stalk-forming agent mainly composed of bacteria, F3 is a stalk-forming agent mainly composed of actinomycetes, urea has a nitrogen content of 46%, and the organic-inorganic compound fertilizer has a nitrogen-phosphorus-potassium content of 17-15-8, organic matter>10 percent of iron fertilizer is FeSO 4 ·H 2 O。|[0063] 1. Influence of different stalk rot types on rice field soil nutrients and active organic carbon libraries|[0064] Test site: lujiang county Guo Hezhen south country village in Anhui province|[0065] The test mode is as follows: field test|[0066] Test material: soil for paddy rice, commercial stalk rot agent, organic-inorganic compound fertilizer, urea, paddy rice seed and the like|[0067] The test steps are as follows:|[0068] 1) Harvesting and returning the straws to the field;|[0069] 2) Applying base fertilizer (according to soil testing formula fertilization scheme, N-P) 2 O 5 -K 2 O=18-6-9 kg/mu, the nitrogen fertilizer consumption is 40%, the organic-inorganic compound fertilizer contains 17-15-8 of nitrogen, phosphorus and potassium, and organic matter>10%, nitrogen content of urea 46%);|[0070] 3) Activating and applying (F1, F2, F3) stalk rot agent;|[0071] 4) Mechanical shallow rotation and irrigation;|[0072] 5) Transplanting and topdressing (60% of the residual nitrogen fertilizer topdressing in the tillering stage).|[0073] The test mainly compares:|[0074] 1) Returning the straw to the field and carrying out soil measurement formula fertilization, wherein the CK is marked;|[0075] 2) Returning straw to the field, testing soil, formulated fertilization and straw rotting agent F1, and marking as SF1;|[0076] 3) Returning straw to the field, testing soil, formulated fertilization and straw rotting agent F2, and marking as SF2;|[0077] 4) Straw returning, soil testing formulated fertilization and straw rotting agent F3, and is marked as SF3.|[0078] Test results:|[0079] as shown in fig. 1, the L I, CPI and CPM I values of the treatment with the stalk agent No. 1 (SF 1) were significantly improved by 11.1%, 11.8% and 24.4% (P < 0.05), respectively.|[0080] As shown in fig. 2, the CPI and CPM I values for SF2 treatment were significantly improved by 11.8% and 22.4%, respectively.|[0081] (P<0.05)。|[0082] As shown in fig. 3, SF3 treated L I, CPI and CPM I were reduced by 1.9%, 3.5% and 5.2%, respectively, with insignificant differences.|[0083] The influence of the change trend of the carbon library of the rice soil under different straw-rotting agent treatment conditions is as follows: SF1> SF2> SF3> CK.|[0084] As shown in table 1, the alkaline hydrolysis nitrogen content of the soil treated by the decomposition agents No. 1 (SF 1) and No. 2 (SF 2) was increased by 14.3% and 15.6%, respectively, and the difference was significant (P < 0.05).|[0085] TABLE 1 Effect of different treatments on the Main nutrient content of soil|[0086] |[0087] 2. Influence of different C/N on decomposition of wheat straw and organic carbon content of soil in rice field:|[0088] test site: lujiang county Guo Hezhen south country village in Anhui province|[0089] The test mode is as follows: field test|[0090] Test material: soil for paddy rice, commercial stalk rot agent, organic-inorganic compound fertilizer, urea, paddy rice seed and the like|[0091] The test steps are as follows:|[0092] 1) Harvesting and returning the straws to the field;|[0093] 2) Applying base fertilizer (according to soil testing formula fertilization scheme, N-P) 2 O 5 -K 2 O=18-6-9 kg/mu, the content of nitrogen, phosphorus and potassium in the organic-inorganic compound fertilizer is 17-15-8, and the organic matter is>10%, the nitrogen content of urea is 46%, and the nitrogen fertilizer dosage is adjusted according to the carbon-nitrogen ratio and the dosage of straw so that the initial C/N is 105:1, 52:1, 18:1 and 12:1 respectively;|[0094] 3) Applying a stalk rot agent (F2);|[0095] 4) Mechanical shallow rotation and irrigation;|[0096] 5) Transplanting and topdressing (dressing the residual total nitrogen fertilizer and FeSO for the base fertilizer in tillering stage) 4 ·H 2 O7 kg/mu).|[0097] The test mainly compares:|[0098] 1) Returning the straws to the field, not applying fertilizer and using a straw-rotting agent F2, wherein the returning C/N ratio is 105:1, and the mark is CN105;|[0099] 2) Straw returning, base reduction, topdressing and straw decomposition agent F2, returning C/N ratio of 24:1, and base fertilizer application N of 70.0kg/hm 2 、P 2 O 5 90kg/hm 2 、K 2 O135kg/hm 2 Tillering fertilizer application N200.00kg/hm 2 Labeled CN24;|[0100] 3) Straw returning, soil testing formulated fertilization and straw rotting agent F2, returning C/N ratio of 18:1, and base fertilizer application of 120kg/hm 2 、P 2 O 5 90kg/hm 2 、K 2 O135kg/hm 2 Tillering fertilizer is applied with N150kg/hm 2 Labeled CN18;|[0101] 4) Straw returning, base increasing and fertilizer additional application and straw decomposition agent F2, returning C/N ratio of 12:1, and base fertilizer application of N150.00kg/hm 2 、P 2 O 5 90kg/hm 2 、K 2 O135kg/hm 2 Tillering fertilizer is applied with N120kg/hm 2 Labeled CN12.|[0102] Test results:|[0103] as shown in FIGS. 4-8, the levels of soil L I, CPI and CMPI perform best when C/N is 18.|[0104] 3. Influence of different moisture management measures on methane emission of paddy field under straw corrosion promotion and returning|[0105] Test site: agricultural garden with high and new technology in university of Anhui agriculture|[0106] The test mode is as follows: field test|[0107] Test material: soil, fertilizer, rice seed, etc. for paddy rice|[0108] The test steps are as follows:|[0109] 1) Crushing and returning the straws to the field;|[0110] 2) Applying base fertilizer (according to soil testing formula fertilization scheme, N-P) 2 O 5 -K 2 O=12-5-6 kg/mu, nitrogen fertilizer accounting for 40%, and organic-inorganic compound fertilizer with nitrogen, phosphorus and potassium content of 17-15-8 and organic matter>10%, nitrogen content of urea 46%);|[0111] 3) Applying a stalk rot agent (F2);|[0112] 4) Mechanical shallow rotation and irrigation regulation;|[0113] 5) Transplanting and topdressing (residual total nitrogen fertilizer and FeSO4.H2O7 kg/mu for topdressing base fertilizer in tillering stage).|[0114] The test mainly compares:|[0115] (1) Conventional irrigation (normal irrigation, tillering and later-stage field sunning of a flooded rice field, natural drying in a yellow ripe stage until harvesting, and maintaining a water layer of 20-50 mm on the field surface at other times in a growing period);|[0116] (2) Controlling irrigation (controlling irrigation, at present, advanced water-saving irrigation technology), wherein the field surface of the controlled irrigation paddy field is kept 5-25mm Bao Shuiceng in the returning period, the water content of root layer soil is used as an irrigation control index in each growth period, and a water layer is not established on the field surface after irrigation).|[0117] Test results:|[0118] as shown in Table 2, the water layer in the water returning period is 5-25mm, no water layer (except for rainfall) is built up except for fertilization, pesticide spraying and weeding, and the water content of the soil volume of the paddy field is used as the regulation index of irrigation, and compared with the conventional irrigation (flooding and medium-term baking), the paddy field CH 4 The discharge amount is obviously reduced by more than 60 percent.|[0119] TABLE 2 Rice field CH 4 Variation of discharge amount|[0120] |[0121] |[0122] 4. Influence of different cultivation depths on organic carbon content of paddy field soil under straw corrosion promotion|[0123] Test site: agricultural garden with high and new technology in university of Anhui agriculture|[0124] The test mode is as follows: field test|[0125] Test material: soil for paddy rice, organic fertilizer, chemical fertilizer, paddy rice seed, etc|[0126] The test steps are as follows:|[0127] 1) Harvesting and returning the straws to the field;|[0128] 2) Applying base fertilizer (according to soil testing formula fertilization scheme, N-P) 2 O 5 -K 2 O=12-5-6 kg/mu, nitrogen fertilizer accounting for 40%, and organic-inorganic compound fertilizer with nitrogen, phosphorus and potassium content of 17-15-8 and organic matter>10%; urea with a nitrogen content of 46%);|[0129] 3) Applying a stalk rot agent (F2);|[0130] 4) Mechanical turning regulation and irrigation;|[0131] 5) Transplanting and topdressing (residual total nitrogen fertilizer and FeSO4.H2O7 kg/mu for topdressing base fertilizer in tillering stage).|[0132] The test mainly compares:|[0133] 1) Straw rotary tillage returning, and is marked as RT;|[0134] 2) Turning over and returning the straw to the field, and marking as CT;|[0135] 3) Turning over the straw without returning to the field, and marking as CT0;|[0136] shallow rotary depth 8cm, rotary tillage depth 11cm, and ploughing depth 18cm.|[0137] Test results:|[0138] the different modes of returning the straws to the field have obvious influence on the SOC contents of different soil layers, mainly related to cultivation depth, and RT and CT are respectively improved by 0-10cm and 10-20cm, so that the straw returning is beneficial to improving the SOC contents by 0-20cm, the straw returning is remarkably improved by 0-20cm in depth, and the soil organic carbon reserves are good in carbon fixing effect.|[0139] TABLE 3 organic carbon reserves of equal quality soil treated by straw returning method|[0140] |[0141] |[0142] The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the above-described embodiments, and that the above-described embodiments and descriptions are only preferred embodiments of the present invention, and are not intended to limit the invention, and that various changes and modifications may be made therein without departing from the spirit and scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof. (CN116784039)|TECHNICAL FIELD|[0001] The invention relates to the field of straw returning, in particular to a method for rapidly improving organic carbon in soil of Jianghuai paddy fields based on straw corrosion promotion and returning.|BACKGROUND ART|[0002] The straw contains nutrient elements necessary for the growth of crops such as carbon, nitrogen, phosphorus, potassium and the like. The annual yield of straw in China is counted to be more than 10 hundred million tons. In recent years, straw is used as a renewable resource to be returned to the field for use in agricultural production, so that the purposes of fertility improvement, synergy and yield improvement, environmental protection and the like can be realized, and straw returning is an important agronomic measure for recycling straw resources. The organic carbon in the soil is taken as one of important soil components, and has important significance for improving agricultural productivity and realizing land carbon balance. A large number of researches show that the straw returning can obviously improve the organic carbon content of soil, improve the quality of organic carbon and provide important guarantee for improving the carbon fixation and emission reduction of farmlands.|[0003] However, it has also been reported that the straw, especially the straw of gramineous crops, is returned to the field in the current year, and if the returning condition is not properly controlled, the straw which is not thoroughly decomposed can cause adverse effect on the growth of the crops, so that the phenomenon of yield reduction occurs. Therefore, agricultural scientists at home and abroad research on the problems of complex molecular structure, unbalanced C/N ratio, poor single microbial degradation effect and the like of the straws, and point out that the microbial inoculum rich in lignocellulose degrading microorganisms is added in the straw degradation process, so that the straw degradation process in the field in the season can be quickened, the degradation time is shortened, and the adverse effect of direct straw returning to the field on next crop is reduced. However, the stalk rot is difficult to exert and stably obtain ideal results due to the effect of the stalk rot caused by various factors such as decomposition mode, regional climate, soil characteristics, antagonism/synergistic effect of indigenous microorganisms and the like. It is not clear whether the accumulation effect of functional microorganisms in the stalk rot is to the organic matters in the soil of the Jianghuai coastal paddy field after the functional microorganisms are added.|[0004] The paddy fields along the sides of Jianghuai generally have the problems of poor physical properties of soil, weak capacity of regulating and storing water, low fertility level, unbalanced nutrient input, massive incineration and piling of crop straw resources and the like. The former people aim at a large number of soil fertility tests which are carried out on Jianghuai coastal paddy fields. The result shows that the organic carbon content of the soil can be effectively improved by carrying out the straw and chemical fertilizer distribution for a long time, but the influence of the straw returning and the straw-decomposing agent distribution on the carbon fixation effect of the soil is still unclear.|[0005] To sum up, in order to promote the organic carbon content of paddy field soil in Jianghuai region and promote the sustainable development of agriculture in the region, further development and improvement of the technology for promoting the decay of rice stubble straw and returning to the field and fixing carbon are needed.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to provide a method for rapidly improving organic carbon in soil of a Jianghuai paddy field based on straw decay promotion and returning to the field, so as to solve the technical problem that the influence of straw decay agent under straw returning to the field on the carbon fixation effect of soil is still unknown.|[0007] The invention aims to solve the technical problems, and is realized by adopting the following technical scheme:|[0008] a method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning comprises the following operation steps:|[0009] s1, crushing straw: harvesting by using a combine harvester with a cutting device, so that the length of the chopped straw is less than 10cm, and the height of the stubble is less than 10cm;|[0010] s2, base fertilizer application and C/N ratio regulation: applying fertilizers according to a proposal of local soil testing formula fertilization, and selecting two fertilizers of organic and inorganic compound fertilizers and urea, wherein the nitrogen consumption of the base fertilizer is required to be adjusted by combining the C/N ratio and the consumption of the straws, so that the initial C/N ratio of the returned straws is (16-20): 1;|[0011] s3, selecting and applying a stalk rot agent: selecting a stalk rot agent which can keep higher activity under the conditions of high temperature of 25-35 ℃ and pH of 5.0-7.5 and intermittent flooding, and uniformly spraying the stalk rot agent on the returning stalks after activating and diluting according to the dosage of 2kg per mu;|[0012] s4, shallow rotation and irrigation: shallow-rotating the straw, organic and inorganic compound fertilizer, urea, stalk rot and the like on the field into soil by using a rotary cultivator, wherein the rotary cultivation depth is controlled to be 5-15cm; then irrigation is carried out, a thin water layer with the thickness of 5-25mm is reserved on the field surface in the green-returning period, the volume water content of the rice field is used as an irrigation regulation index, and the water layer is not established on the field surface after irrigation;|[0013] s5, transplanting rice seedlings, topdressing and soil carbon fixation efficiency excitation: transplanting rice seedlings after irrigation is finished, applying a residual nitrogen fertilizer by dressing a base fertilizer in a tillering stage of the rice, and simultaneously applying FeSO (FeSO) according to 5-10 kg/mu in a region with an effective iron background value of soil lower than 10mg/kg 4 ·H 2 O。|[0014] Preferably, the organic-inorganic compound fertilizer N in step S1: p (P) 2 O 5 :K 2 The O ratio is 17%:15%:8% of organic matters of the organic-inorganic compound fertilizer>10%。|[0015] Preferably, the stalk rot agent functional microorganism in the step S3 is mainly fungi.|[0016] Preferably, the stalk agent in step S3 is activated and diluted according to 1:100 was dissolved in water and incubated at 30℃for 24 hours.|[0017] Preferably, the iron fertilizer in step S5 isFerrous sulphate is used in a specific amount in combination with the effective iron content of the local soil (less than 10 mg/kg), typically required FeSO to be applied 4 ·H 2 O7 kg/mu.|[0018] Preferably, the stalk agent spraying device in the step S3 is an agent spraying device, the agent spraying device and the rotary cultivator in the step S4 are of an integrated structure, the rotary cultivator comprises a rotary cultivation mechanism, material containing pieces arranged on two sides of the top end of the rotary cultivation mechanism, one ends of the two material containing pieces are respectively provided with a transmission piece connected with the rotary cultivation mechanism, the bottom ends of the two material containing pieces are respectively provided with a spraying pipe extending to one side, the side surfaces of the two material containing pieces are respectively provided with a pressing piece, and one end of the pressing piece is provided with a linkage piece connected with the transmission piece;|[0019] the rotary tillage mechanism comprises a rotary tillage mechanism body, and is characterized in that the material containing piece comprises a material barrel fixed at the top end of the rotary tillage mechanism, a connecting shaft penetrating through the material barrel and connected with the transmission piece is rotationally arranged in the middle of the material barrel, and a plurality of stirring blades are sleeved on the outer side of the connecting shaft and the inner side of the material barrel.|[0020] Preferably, the pressurizing member comprises a shell fixed on the side surface of the material containing member, a screw rod penetrating through the shell and connected with the linkage member is rotationally arranged in the middle of the shell, a piston connected with the shell is sleeved on the outer side of the screw rod and the inner side of the shell, an air inlet valve is arranged at one end of the shell, and an air outlet valve connected with the material barrel is arranged at one end of the shell and positioned at one side of the air inlet valve.|[0021] Preferably, the spraying pipe comprises a hose with a spray head, a valve arranged in the middle of the hose, and a support rod arranged at one end of the hose and above the spray head of the hose.|[0022] Preferably, baffle plates which are arranged at equal angles are arranged on two sides of the stirring blade, and a plurality of shearing teeth are arranged on the edge of the stirring blade.|[0023] Preferably, the screw rod is a reciprocating screw rod.|[0024] The beneficial effects of the invention are as follows:|[0025] 1. the method for rapidly improving organic carbon in soil of the Jianghuai paddy field based on straw corrosion promotion and returning is remarkable in soil improvement effect, capable of improving the variability of organic matters in soil of a cultivated layer, and meanwhile capable of effectively improving the organic carbon reserves of the soil, and good in carbon fixing effect.|[0026] 2. The method for rapidly improving organic carbon in soil of the Jianghuai paddy field based on straw corrosion promotion and returning to the field is simple in procedure, convenient to operate, capable of being completed by general growers, and beneficial to large-scale popularization of the technology.|[0027] 3. According to the rotary tillage machine, spraying and rotary tillage are integrated, the rotary tillage rotating shaft is linked with the screw rod through the transmission piece, the linkage piece and the connecting shaft, when the rotary tillage rotating shaft rotates, the connecting shaft and the screw rod simultaneously rotate, the connecting shaft drives the stirring blade, the stalk rot agent at the inner side of the feed cylinder is mixed with water, the phenomenon of precipitation or layering when liquid medicine moves is avoided, the screw rod drives the piston to reciprocate, the air pressure is supplemented at the inner side of the feed cylinder by matching with the air outlet valve and the air inlet valve, the liquid medicine is prevented from being sprayed by a water pump, the time of spraying rotary tillage is improved, and the straw returning efficiency is improved.|DRAWINGS DESCRIPTION|[0028] FIG. 1 is a schematic diagram showing the effect of different stalk agent treatments on L I content according to the present invention;|[0029] FIG. 2 is a schematic diagram showing the effect of different stalk agent treatments of the present invention on CPI content;|[0030] FIG. 3 is a schematic illustration of the effect of different stalk agent treatments of the present invention on CMPI content;|[0031] FIG. 4 is a schematic diagram showing the effect of different carbon-nitrogen ratio treatments on straw decomposition rate;|[0032] FIG. 5 is a graph showing the effect of different carbon to nitrogen ratio treatments of the present invention on total organic carbon content;|[0033] FIG. 6 is a graph showing the effect of different carbon to nitrogen ratio treatments on L I content according to the present invention;|[0034] FIG. 7 is a graph showing the effect of different carbon to nitrogen ratio treatments of the present invention on CPI content;|[0035] FIG. 8 is a graph showing the effect of different carbon to nitrogen ratio treatments on CMPI content in accordance with the present invention;|[0036] FIG. 9 is a schematic view of the spraying and rotary tillage configuration of the present invention;|[0037] FIG. 10 is a schematic view of a spray tube according to the present invention;|[0038] FIG. 11 is a schematic cross-sectional view of a pod of the present invention;|[0039] FIG. 12 is a schematic cross-sectional view of a compression member of the present invention;|[0040] reference numerals: 1. a rotary tillage mechanism; 2. a spraying tube; 21. a hose; 22. a valve; 23. a support rod; 3. a transmission member; 4. a material containing piece; 41. a charging barrel; 42. a connecting shaft; 43. stirring the leaves; 5. a linkage member; 6. a pressurizing member; 61. a housing; 62. a piston; 63. a screw rod; 64. an air outlet valve; 65. an air inlet valve.|INVENTION MODE|Detailed Description|[0041] In order that the manner in which the above recited features, objects and advantages of the present invention are obtained, a more particular description of the invention will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings. Based on the examples in the embodiments, those skilled in the art can obtain other examples without making any inventive effort, which fall within the scope of the invention.|[0042] Specific embodiments of the present invention are described below with reference to the accompanying drawings.|[0043] Example 1|[0044] A method for rapidly improving organic carbon in soil of Jianghuai paddy field based on straw decay promotion and returning comprises the following operation steps:|[0045] s1, crushing straw: harvesting the straw crops in the regions from the last 5 months to the last 6 months of the year by using a combine harvester with a cutting device after the straw crops in the regions of Jianghuai are ripe, so that the length of the cut straw is less than 10cm and the stubble height is less than 10cm;|[0046] s2, base fertilizer application and C/N ratio regulation: applying fertilizers according to a local soil testing formula fertilization proposal, and selecting two fertilizers of organic and inorganic compound fertilizers and urea, wherein the nitrogen consumption of the base fertilizer is required to be adjusted by combining the C/N ratio and the consumption of the straws, so that the initial C/N ratio of the returned straws is 18:1;|[0047] s3, selecting and applying a stalk rot agent: selecting a stalk rot agent which can keep higher activity under the conditions of high temperature of 25-35 ℃ and pH of 5.0-7.5 and intermittent flooding, and uniformly spraying the stalk rot agent on the returning stalks after activating and diluting according to the dosage of 2kg per mu;|[0048] s4, shallow rotation and irrigation: shallow-rotating the straw, organic and inorganic compound fertilizer, urea, stalk-rotting agent and the like on the field into soil by using a rotary cultivator, wherein the rotary cultivation depth is controlled at 10cm; then irrigation is carried out, a thin water layer with the thickness of 15mm is reserved on the field surface in the green-returning period, the volume water content of the rice field is used as an irrigation regulation index, and the water layer is not established on the field surface after irrigation;|[0049] s5, transplanting rice seedlings, topdressing and soil carbon fixation efficiency excitation: transplanting rice seedlings after irrigation is finished, applying a residual nitrogen fertilizer by dressing a base fertilizer in a tillering stage of the rice, and simultaneously applying FeSO (FeSO) according to 5-10 kg/mu in a region with an effective iron background value of soil lower than 10mg/kg 4 ·H 2 O to promote the soil carbon fixation efficiency.|[0050] Wherein, the organic-inorganic compound fertilizer N in the step S2: p (P) 2 O 5 :K 2 The O ratio is 17%:15%:8% of organic matters of the organic-inorganic compound fertilizer>10%。|[0051] Wherein the stalk rot agent functional microorganism in the step S3 is mainly fungi.|[0052] Wherein, the stalk agent in the step S3 is activated and diluted according to the following formula 1:100 was dissolved in water and incubated at 30℃for 24 hours.|[0053] Wherein the iron fertilizer in the step S5 is ferrous sulfate, the specific dosage is combined with the effective iron content (lower than 10 mg/kg) of the local soil, and FeSO is generally required to be applied 4 ·H 2 O7 kg/mu.|[0054] The stalk agent spraying device in the step S3 is an agent spraying device, the agent spraying device and the rotary cultivator in the step S4 are of an integrated structure, the rotary cultivator comprises a rotary tillage mechanism 1, material containing pieces 4 arranged on two sides of the top end of the rotary tillage mechanism 1, one ends of the two material containing pieces 4 are respectively provided with a transmission piece 3 connected with the rotary tillage mechanism 1, the bottom ends of the two material containing pieces 4 are respectively provided with a spraying pipe 2 extending to one side, the side surfaces of the two material containing pieces 4 are respectively provided with a pressing piece 6, and one end of the pressing piece 6 is provided with a linkage piece 5 connected with the transmission piece 3;|[0055] the material containing piece 4 comprises a material barrel 41 fixed at the top end of the rotary tillage mechanism 1, a connecting shaft 42 penetrating through the material barrel 41 and connected with the transmission piece 3 is rotatably arranged in the middle of the material barrel 41, and a plurality of stirring blades 43 are sleeved on the outer side of the connecting shaft 42 and the inner side of the material barrel 41.|[0056] The pressurizing member 6 includes a housing 61 fixed on the side of the material containing member 4, a screw rod 63 penetrating the housing 61 and connected with the linkage member 5 is rotatably disposed in the middle of the housing 61, a piston 62 connected with the housing 61 is sleeved on the outer side of the screw rod 63 and on the inner side of the housing 61, an air inlet valve 65 is disposed at one end of the housing 61, and an air outlet valve 64 connected with the barrel 41 is disposed at one end of the housing 61 and on one side of the air inlet valve 65.|[0057] Wherein, the spraying pipe 2 comprises a hose 21 with a spray head, a valve 22 arranged in the middle of the hose 21, and a support rod 23 arranged at one end of the hose 21 and above the spray head of the hose 21.|[0058] Wherein, both sides of stirring leaf 43 all are equipped with the baffle that equiangular arrangement, and stirring leaf 43's edge is equipped with a plurality of shearing teeth.|[0059] Wherein the screw 63 is a reciprocating screw.|[0060] As shown in fig. 9-12, in this embodiment, by mounting the material containing member 4 on the rotary tillage mechanism 1 and connecting the material containing member 4 with the rotary tillage mechanism 1 through the transmission member 3, when the rotary tillage mechanism 1 performs rotary tillage, the rotating shaft drives the connecting shaft 42 through the transmission member 3, the connecting shaft 42 drives the stirring blade 43 to rotate at the inner side of the charging barrel 41, the stirring blade 43 mixes the stalk-melting agent at the inner side of the charging barrel 41 with water, and the shearing blade at the edge of the stirring blade 43 improves the uniformity of dispersing the stalk-melting agent in water, simultaneously the transmission member 3 drives the linkage member 5 to operate, the linkage member 5 drives the screw 63 to rotate at the inner side of the housing 61, the piston 62 reciprocates according to the groove on the surface of the screw 63, and simultaneously air between the piston 62 and the housing 61 and the inner side of the pressing charging barrel 41 are pressed through the air outlet valve 64, the inner side of the charging barrel 41 has pressure, and the stalk-melting agent is sprayed through the nozzle of the hose 21 when the valve 22 is opened, so that the stalk-melting efficiency is increased, and the stalk-melting agent needs to be conveyed by the pump.|[0061] The following comparative experiments were carried out on the method for rapidly improving organic carbon in soil of Jianghuai paddy field by promoting straw to decay and returning to field in the present example:|[0062] in this example, F1 is a stalk-forming agent mainly composed of bacteria, F2 is a stalk-forming agent mainly composed of bacteria, F3 is a stalk-forming agent mainly composed of actinomycetes, urea has a nitrogen content of 46%, and the organic-inorganic compound fertilizer has a nitrogen-phosphorus-potassium content of 17-15-8, organic matter>10 percent of iron fertilizer is FeSO 4 ·H 2 O。|[0063] 1. Influence of different stalk rot types on rice field soil nutrients and active organic carbon libraries|[0064] Test site: lujiang county Guo Hezhen south country village in Anhui province|[0065] The test mode is as follows: field test|[0066] Test material: soil for paddy rice, commercial stalk rot agent, organic-inorganic compound fertilizer, urea, paddy rice seed and the like|[0067] The test steps are as follows:|[0068] 1) Harvesting and returning the straws to the field;|[0069] 2) Applying base fertilizer (according to soil testing formula fertilization scheme, N-P) 2 O 5 -K 2 O=18-6-9 kg/mu, the nitrogen fertilizer consumption is 40%, the organic-inorganic compound fertilizer contains 17-15-8 of nitrogen, phosphorus and potassium, and organic matter>10%, nitrogen content of urea 46%);|[0070] 3) Activating and applying (F1, F2, F3) stalk rot agent;|[0071] 4) Mechanical shallow rotation and irrigation;|[0072] 5) Transplanting and topdressing (60% of the residual nitrogen fertilizer topdressing in the tillering stage).|[0073] The test mainly compares:|[0074] 1) Returning the straw to the field and carrying out soil measurement formula fertilization, wherein the CK is marked;|[0075] 2) Returning straw to the field, testing soil, formulated fertilization and straw rotting agent F1, and marking as SF1;|[0076] 3) Returning straw to the field, testing soil, formulated fertilization and straw rotting agent F2, and marking as SF2;|[0077] 4) Straw returning, soil testing formulated fertilization and straw rotting agent F3, and is marked as SF3.|[0078] Test results:|[0079] as shown in fig. 1, the L I, CPI and CPM I values of the treatment with the stalk agent No. 1 (SF 1) were significantly improved by 11.1%, 11.8% and 24.4% (P < 0.05), respectively.|[0080] As shown in fig. 2, the CPI and CPM I values for SF2 treatment were significantly improved by 11.8% and 22.4%, respectively.|[0081] (P<0.05)。|[0082] As shown in fig. 3, SF3 treated L I, CPI and CPM I were reduced by 1.9%, 3.5% and 5.2%, respectively, with insignificant differences.|[0083] The influence of the change trend of the carbon library of the rice soil under different straw-rotting agent treatment conditions is as follows: SF1> SF2> SF3> CK.|[0084] As shown in table 1, the alkaline hydrolysis nitrogen content of the soil treated by the decomposition agents No. 1 (SF 1) and No. 2 (SF 2) was increased by 14.3% and 15.6%, respectively, and the difference was significant (P < 0.05).|[0085] TABLE 1 Effect of different treatments on the Main nutrient content of soil|[0086] |[0087] 2. Influence of different C/N on decomposition of wheat straw and organic carbon content of soil in rice field:|[0088] test site: lujiang county Guo Hezhen south country village in Anhui province|[0089] The test mode is as follows: field test|[0090] Test material: soil for paddy rice, commercial stalk rot agent, organic-inorganic compound fertilizer, urea, paddy rice seed and the like|[0091] The test steps are as follows:|[0092] 1) Harvesting and returning the straws to the field;|[0093] 2) Applying base fertilizer (according to soil testing formula fertilization scheme, N-P) 2 O 5 -K 2 O=18-6-9 kg/mu, the content of nitrogen, phosphorus and potassium in the organic-inorganic compound fertilizer is 17-15-8, and the organic matter is>10%, the nitrogen content of urea is 46%, and the nitrogen fertilizer dosage is adjusted according to the carbon-nitrogen ratio and the dosage of straw so that the initial C/N is 105:1, 52:1, 18:1 and 12:1 respectively;|[0094] 3) Applying a stalk rot agent (F2);|[0095] 4) Mechanical shallow rotation and irrigation;|[0096] 5) Transplanting and topdressing (dressing the residual total nitrogen fertilizer and FeSO for the base fertilizer in tillering stage) 4 ·H 2 O7 kg/mu).|[0097] The test mainly compares:|[0098] 1) Returning the straws to the field, not applying fertilizer and using a straw-rotting agent F2, wherein the returning C/N ratio is 105:1, and the mark is CN105;|[0099] 2) Straw returning, base reduction, topdressing and straw decomposition agent F2, returning C/N ratio of 24:1, and base fertilizer application N of 70.0kg/hm 2 、P 2 O 5 90kg/hm 2 、K 2 O135kg/hm 2 Tillering fertilizer application N200.00kg/hm 2 Labeled CN24;|[0100] 3) Straw returning, soil testing formulated fertilization and straw rotting agent F2, returning C/N ratio of 18:1, and base fertilizer application of 120kg/hm 2 、P 2 O 5 90kg/hm 2 、K 2 O135kg/hm 2 Tillering fertilizer is applied with N150kg/hm 2 Labeled CN18;|[0101] 4) Straw returning, base increasing and fertilizer additional application and straw decomposition agent F2, returning C/N ratio of 12:1, and base fertilizer application of N150.00kg/hm 2 、P 2 O 5 90kg/hm 2 、K 2 O135kg/hm 2 Tillering fertilizer is applied with N120kg/hm 2 Labeled CN12.|[0102] Test results:|[0103] as shown in FIGS. 4-8, the levels of soil L I, CPI and CMPI perform best when C/N is 18.|[0104] 3. Influence of different moisture management measures on methane emission of paddy field under straw corrosion promotion and returning|[0105] Test site: agricultural garden with high and new technology in university of Anhui agriculture|[0106] The test mode is as follows: field test|[0107] Test material: soil, fertilizer, rice seed, etc. for paddy rice|[0108] The test steps are as follows:|[0109] 1) Crushing and returning the straws to the field;|[0110] 2) Applying base fertilizer (according to soil testing formula fertilization scheme, N-P) 2 O 5 -K 2 O=12-5-6 kg/mu, nitrogen fertilizer accounting for 40%, and organic-inorganic compound fertilizer with nitrogen, phosphorus and potassium content of 17-15-8 and organic matter>10%, nitrogen content of urea 46%);|[0111] 3) Applying a stalk rot agent (F2);|[0112] 4) Mechanical shallow rotation and irrigation regulation;|[0113] 5) Transplanting and topdressing (residual total nitrogen fertilizer and FeSO4.H2O7 kg/mu for topdressing base fertilizer in tillering stage).|[0114] The test mainly compares:|[0115] (1) Conventional irrigation (normal irrigation, tillering and later-stage field sunning of a flooded rice field, natural drying in a yellow ripe stage until harvesting, and maintaining a water layer of 20-50 mm on the field surface at other times in a growing period);|[0116] (2) Controlling irrigation (controlling irrigation, at present, advanced water-saving irrigation technology), wherein the field surface of the controlled irrigation paddy field is kept 5-25mm Bao Shuiceng in the returning period, the water content of root layer soil is used as an irrigation control index in each growth period, and a water layer is not established on the field surface after irrigation).|[0117] Test results:|[0118] as shown in Table 2, the water layer in the water returning period is 5-25mm, no water layer (except for rainfall) is built up except for fertilization, pesticide spraying and weeding, and the water content of the soil volume of the paddy field is used as the regulation index of irrigation, and compared with the conventional irrigation (flooding and medium-term baking), the paddy field CH 4 The discharge amount is obviously reduced by more than 60 percent.|[0119] TABLE 2 Rice field CH 4 Variation of discharge amount|[0120] |[0121] |[0122] 4. Influence of different cultivation depths on organic carbon content of paddy field soil under straw corrosion promotion|[0123] Test site: agricultural garden with high and new technology in university of Anhui agriculture|[0124] The test mode is as follows: field test|[0125] Test material: soil for paddy rice, organic fertilizer, chemical fertilizer, paddy rice seed, etc|[0126] The test steps are as follows:|[0127] 1) Harvesting and returning the straws to the field;|[0128] 2) Applying base fertilizer (according to soil testing formula fertilization scheme, N-P) 2 O 5 -K 2 O=12-5-6 kg/mu, nitrogen fertilizer accounting for 40%, and organic-inorganic compound fertilizer with nitrogen, phosphorus and potassium content of 17-15-8 and organic matter>10%; urea with a nitrogen content of 46%);|[0129] 3) Applying a stalk rot agent (F2);|[0130] 4) Mechanical turning regulation and irrigation;|[0131] 5) Transplanting and topdressing (residual total nitrogen fertilizer and FeSO4.H2O7 kg/mu for topdressing base fertilizer in tillering stage).|[0132] The test mainly compares:|[0133] 1) Straw rotary tillage returning, and is marked as RT;|[0134] 2) Turning over and returning the straw to the field, and marking as CT;|[0135] 3) Turning over the straw without returning to the field, and marking as CT0;|[0136] shallow rotary depth 8cm, rotary tillage depth 11cm, and ploughing depth 18cm.|[0137] Test results:|[0138] the different modes of returning the straws to the field have obvious influence on the SOC contents of different soil layers, mainly related to cultivation depth, and RT and CT are respectively improved by 0-10cm and 10-20cm, so that the straw returning is beneficial to improving the SOC contents by 0-20cm, the straw returning is remarkably improved by 0-20cm in depth, and the soil organic carbon reserves are good in carbon fixing effect.|[0139] TABLE 3 organic carbon reserves of equal quality soil treated by straw returning method|[0140] |[0141] |[0142] The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the above-described embodiments, and that the above-described embodiments and descriptions are only preferred embodiments of the present invention, and are not intended to limit the invention, and that various changes and modifications may be made therein without departing from the spirit and scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof. Family Number|(106614910)|106614910|Abstract|(CN116784039 A)|The invention provides a method for rapidly increasing soil organic carbon of a rice field in Jianghuai province based on straw decay promotion and returning , and relates to the field of straw returning , and the method comprises the following operation steps : straw crushing , base fertilizer application and C / N ratio regulation and control , straw decay agent selection and application , shallow rotation and irrigation , rice seedling transplanting , topdressing and soil carbon sequestration efficiency excitation . The ratio of N to P2O5 to K2O in the organic - inorganic compound fertilizer in the step S1 is 17% : 15% : 8%, and the organic - inorganic compound fertilizer contains organic matters gt ; according to the method for rapidly increasing the soil organic carbon of the Jianghuai rice field based on straw decay promotion and field returning , the soil improvement effect is remarkable , the organic matter mutability of soil of a plough layer can be improved , meanwhile , the soil organic carbon storage amount is effectively increased , and the good carbon sequestration effect is achieved ; according to the method for rapidly increasing the soil organic carbon of the Jianghuai rice field based on straw decay promoting and returning , the procedure is simple , operation is convenient , common farmers can complete the method , and large - scale popularization of the technology is facilitated . |CPC codes|(CN116784039 A)|A01B - 049/04 |A01B - 079/00 |A01B - 079/02 |A01C - 021/00 |A01G - 022/22 |IPC codes|(CN116784039 A)|A01B - 049/04 |A01B - 079/00 |A01B - 079/02 |A01C - 021/00 |A01G - 022/22 | Basic materials chemistry|Chemical engineering|Other special machines A01B-049/04|A01B-079/00|A01B-079/02|A01C-021/00|A01G-022/22|B05B-009/047|B05B-015/25|C09K-017/14|C09K-2101/00 A01B-049/04|A01B-079/00|A01B-079/02|A01C-021/00|A01G-022/22|B05B-009/047|B05B-015/25|C09K-017/14|C09K-2101/00 A01B-049/04|A01B-079/00|A01B-079/02|A01C-021/00|A01G-022/22|B05B-009/047|B05B-015/25|C09K-017/14|C09K-101/00 A01B-049/04|A01B-079/00|A01B-079/02|A01C-021/00|A01G-022/22|B05B-009/047|B05B-015/25|C09K-017/14|C09K-101/00 CN120858693 CN120858693 116500001 WHO=Examiner SELF=N CAT=A CN108990459|CN208425157U|CN218998858U|US20210300836|KR20210035992 CN108990459 82497469 WHO=Examiner SELF=N CAT=Y CAT=X|CN208425157U 83183426 WHO=Examiner SELF=N CAT=Y|CN218998858U 104931449 WHO=Examiner SELF=N CAT=A|US20210300836 89797717 WHO=Examiner SELF=N CAT=A|KR20210035992 93410677 WHO=Examiner SELF=N CAT=A CN108990459; CN208425157U; KR20210035992; US20210300836; CN218998858U REVOKED (CN116784039)|REVOKED DEAD (CN116784039)|DEAD (CN116784039)|LEGAL DETAILS FOR CN116784039|Actual or expected expiration date=2026-03-20|Legal state=DEAD|Status=REVOKED|Event publication date=2023-06-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202310772359|Application date=2023-06-28|Standardized application number=2023CN-0772359|Event publication date=2023-09-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN116784039|Publication stage code=A|Publication date=2023-09-22|Standardized publication number=CN116784039|Event publication date=2023-09-22|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-10-13|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2026-03-20|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTA6XoSHYw6eVfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000069591434&ekey=2116&xpn=CN116784039&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=SYd%252FuSiW185wTCdd%252BxQSyZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN116784039)|CN (CN116784039)|NAME=ANHUI AGRICULTURAL UNIVERSITY , COUNTRY=CN (CN116784039)|NAME=WU QI;Hefei Lawong Patent Agency (General Partnership) , REG=34140 (CN116784039)|NAME=MA CHAO|NAME=SHI XINYI|NAME=WU ZELU|NAME=LU MENGXING|NAME=TANG YUEYUE|NAME=GUO MENGMENG|NAME=LIU ZIXIN|NAME=WEI ZHENGYU|NAME=ZHU LIN 0 1 Titre: (CN116784039)|Method for rapidly increasing soil organic carbon in Jianghuai rice field based on straw decay promotion and returning Résumé: (CN116784039)|The invention provides a method for rapidly increasing soil organic carbon of a rice field in Jianghuai province based on straw decay promotion and returning, and relates to the field of straw returning, and the method comprises the following operation steps: straw crushing, base fertilizer application and C/N ratio regulation and control, straw decay agent selection and application, shallow rotation and irrigation, rice seedling transplanting, topdressing and soil carbon sequestration efficiency excitation. The ratio of N to P2O5 to K2O in the organic-inorganic compound fertilizer in the step S1 is 17%: 15%: 8%, and the organic-inorganic compound fertilizer contains organic matters gt; according to the method for rapidly increasing the soil organic carbon of the Jianghuai rice field based on straw decay promotion and field returning, the soil improvement effect is remarkable, the organic matter mutability of soil of a plough layer can be improved, meanwhile, the soil organic carbon storage amount is effectively increased, and the good carbon sequestration effect is achieved; according to the method for rapidly increasing the soil organic carbon of the Jianghuai rice field based on straw decay promoting and returning, the procedure is simple, operation is convenient, common farmers can complete the method, and large-scale popularization of the technology is facilitated. 56 Abstract gpt-4o-mini no The article focuses on increasing soil organic carbon through straw decay and does not mention mineral weathering or CO₂ capture.
57 CN201921545593U CN201921545593U CN210945175 89579289 CN210945175 U 2020-07-07 [CN210945175U] 2019-09-18 2019-09-18 2020-07-07 (CN210945175U)|2020-07-07 (CN210945175)|2021-09-18 (CN210945175)|Food sewage treatment device with crushing function (CN210945175)|The utility model is suitable for the technical field of sewage treatment. The food sewage treatment device with the crushing function comprises a crushing assembly and a deodorizing assembly, the crushing assembly comprises a box body, a crushing roller, a purifying box and a crusher, the output end of the crusher is in transmission connection with the crushing roller and is fixed in the box body, and the purifying box is fixed under the crushing roller; air with peculiar smell in the box body can be pumped into the through hole through the fan; flow along through holes, activated carbon adsorption rod, adsorption using activated carbon, removal of odors in air, the treated air is continuously conveyed into the box body through the through holes; according to the air purification device,air with peculiar smell is continuously pumped, purified and input, so that the peculiar smell in the box body can be continuously desalted, and meanwhile, a worker can take down the mounting plate and replace the activated carbon adsorption rods in the through holes, so that subsequent peculiar smell removal can be smoothly carried out. NANTONG VOCATIONAL COLLEGE (CN210945175)|NANTONG VOCATIONAL COLLEGE ([CN]) ZHONG JIULONG|YANG LIJUN|DONG YANGQIN|SHU HUI (CN210945175)|ZHONG JIULONG|YANG LIJUN|DONG YANGQIN|SHU HUI (CN210945175)|XU SIBO;BEIJING KEJIA INTELLECTUAL PROPERTY FIRM|Reg. Nb: 11427 (CN210945175)|The utility model provides a food sewage treatment plant with crushing function, when aiming at solving the sewage to food on the existing market and handling, the most rubbish that need in the food sewage is broken to collect the rubbish after the breakage, and the rubbish after the breakage can distribute the peculiar smell equally, and then influences the follow-up processing problem of staff to rubbish.| (CN210945175)|1. The utility model provides a food sewage treatment plant with crushing function, includes broken subassembly (1) and removes flavor component (2), broken subassembly (1) includes box (11), crushing roller (12), purifying box (17) and breaker (19), the output transmission of breaker (19) connect in crushing roller (12) to be fixed in the inside of box (11), purifying box (17) are fixed in under crushing roller (12), its characterized in that: remove flavor subassembly (2) and include fan (22), mounting panel (24) and activated carbon adsorption stick (27), through-hole (26) have been seted up to the inside of box (11), activated carbon adsorption stick (27) accept in inside through-hole (26), just the input and the output of fan (22) all with through-hole (26) are linked together, and are fixed in the outer wall of box (11), just mounting panel (24) can dismantle connect in box (11), and with through-hole (26) mutual adaptation.| (CN210945175)|Referring to fig. 1-4, the present invention provides a technical solution: the utility model provides a food sewage treatment plant with crushing function, include broken subassembly 1 and go flavor subassembly 2, broken subassembly 1 includes box 11, crushing roller 12, purifying box 17 and breaker 19, the output transmission of breaker 19 is connected in crushing roller 12, and be fixed in the inside of box 11, purifying box 17 is fixed in under the crushing roller 12, it includes fan 22 to go flavor subassembly 2, mounting panel 24 and active carbon adsorption stick 27, through-hole 26 has been seted up to the inside of box 11, active carbon adsorption stick 27 is acceptd inside through-hole 26, and fan 22's input and output all are linked together with through-hole 26, and be fixed in the outer wall of box 11, and mounting panel 24 can dismantle and connect in box 11, and with the mutual adaptation of through-hole 26.|The utility model is suitable for the technical field of sewage treatment, and provides a food sewage treatment device with a crushing function, which comprises a crushing component and a deodorizing component, wherein the crushing component comprises a box body, a crushing roller, a purifying box and a crusher; can be with inside the through-hole of the air pump of box that has the peculiar smell through the fan, and flow along the through-hole, when the active carbon adsorption stick, utilize the adsorptivity of active carbon, get rid of the peculiar smell in the air, and the air after the processing just continues to carry the inside of box through the through-hole, continuous pumping to the air that has the peculiar smell afterwards, purify and input, the inside with the peculiar smell of continuous desalination box, and simultaneously, the staff still can take off the mounting panel, and change the active carbon adsorption stick inside the through-hole, make that it can be smooth carry out subsequent peculiar smell and clear away.| (CN210945175)|BOX(100,28)|BOX PURIFICATION(100,21)|CRUSHING ROLLER(100,15)|CRUSHING FUNCTION(100,12)|BROKEN SUBASSEMBLY(100,4)|FOOD SEWAGE TREATMENT PLANT(100,4)|SEWAGE TREATMENT PLANT(100,4)|BREAKER(100,2)|BREAKER OUTPUT TRANSMISSION(100,2)|OUTPUT TRANSMISSION(100,2)|ROLLER(100,2)|DESALINIZATION BOX PECULIAR SMELL(100,1)|PECULIAR SMELL(92,11)|DESALINIZATION BOX(49,1)|FOOD WASTEWATER TREATMENT(46,7)|ACTIVATED CARBON ADSORPTION STICK(44,3)|CRUSHING COMPONENT(39,2)|LINKING PIPE(36,4)|BULL STICK(32,7)|PURPLE LIGHT LAMP(26,12)|MOUNTING PANEL(25,9)|SUBASSEMBLY(25,2)|PUMPING(25,1)|ACTIVE CARBON ADSORPTIVITY(24,1)|DEODORIZING COMPONENT(23,2)|FOOD SEWAGE TREATMENT(23,2)|CENTER GRIPPING(23,1)|ACTIVE CARBON ADSORPTION STICK(20,2)|CRUSHER(19,6)|SEWAGE TREATMENT(17,4)|BREAKER STRAIGHT(17,2)|STAFF(17,2)|FAN(14,8)|FILTER SCREEN(14,6)|BLOCKING PLATE(14,5)|BOX AIR PUMP(14,1)|ACTIVE CARBON ADSORPTION(11,4)|PURIFYING BOX BOTTOM(10,3)|INSIDE CAVITY(10,1)|COLLECTING BOX(9,6)|AIR PUMP(8,1)|DISTINGUISHING FLAVOR SUBASSEMBLY(8,1)|PIPELINE FIXED CONNECTION(8,1)|ACTIVE CARBON(6,2)|MOUNTING PLATE(5,11)|CRUSHING ROLLER BOX(5,1)|CRUSHING SUBASSEMBLY(5,1)|OUTER WALL(4,14)|FOOD WASTE TREATMENT(4,4)|RUBBISH(4,4)|ACTIVATED CARBON ADSORPTION ROD(4,3)|SLIDING MODE(4,2)|CRUSHING ROLLER STRAIGHT(4,1)|MOUNTING PANEL OUTER WALL(3,3)|BREAKAGE(3,2)|BULL(3,2)|ENVIRONMENTAL POLLUTION(3,2)| (CN210945175)|1. The utility model provides a food sewage treatment plant with crushing function, includes broken subassembly (1) and removes flavor component (2), broken subassembly (1) includes box (11), crushing roller (12), purifying box (17) and breaker (19), the output transmission of breaker (19) connect in crushing roller (12) to be fixed in the inside of box (11), purifying box (17) are fixed in under crushing roller (12), its characterized in that: remove flavor subassembly (2) and include fan (22), mounting panel (24) and activated carbon adsorption stick (27), through-hole (26) have been seted up to the inside of box (11), activated carbon adsorption stick (27) accept in inside through-hole (26), just the input and the output of fan (22) all with through-hole (26) are linked together, and are fixed in the outer wall of box (11), just mounting panel (24) can dismantle connect in box (11), and with through-hole (26) mutual adaptation.|2. The food wastewater treatment apparatus with a crushing function according to claim 1, wherein: two openings (21) are arranged on the inner wall of the box body (11) of the crushing roller (12) far away from the crusher (19), and the openings (21) are communicated with the through hole (26).|3. The food wastewater treatment apparatus with a crushing function according to claim 2, wherein: the number of the through holes (26) is four, the four through holes (26) surround the inside of the box body (11), and two ends of the through holes are respectively communicated with the two openings (21).|4. The food wastewater treatment apparatus with a crushing function according to claim 1, wherein: the mounting plate (24) is located the crushing roller (12) is close to one side of breaker (19), just activated carbon adsorption stick (27) centre gripping in mounting plate (24) with between through-hole (26), and be located inside through-hole (26) that mounting plate (24) corresponds.|5. The food wastewater treatment apparatus with a crushing function according to claim 1, wherein: remove flavor subassembly (2) and still include two linking pipes (28), linking pipe (28) are fixed in the outer wall of box (11), and two linking pipe (28) inside cavity and run through the outer wall of box (11), just the input and the output of fan (22) pass through pipeline fixed connection in linking pipe (28) to through linking pipe (28) with through-hole (26) are linked together.|6. The food wastewater treatment apparatus with a crushing function according to claim 1, wherein: the outer wall of mounting panel (24) is fixed and is provided with handle (25), just handle (25) are C shape, and be provided with bull stick (23) directly over mounting panel (24), bull stick (23) rotate through the pivot connect in the outer wall of box (11), just mounting panel (24) pass through bull stick (23) joint in box (11).|7. The food wastewater treatment apparatus with a crushing function according to claim 1, wherein: the crushing assembly (1) further comprises a blocking plate (13), a collecting box (14) and a water discharging pipe (18), the blocking plate (13) is fixed between the crushing roller (12) and the purifying box (17), one end of the water discharging pipe (18) is fixed to the purifying box (17) and communicated with the inside of the purifying box (17), and the collecting box (14) is located at the bottom of the box body (11) and is connected to the box body (11) in a sliding mode.|8. The food wastewater treatment apparatus with a crushing function according to claim 1, wherein: the inside of purifying box (17) is equipped with filter screen (15) and purple light lamp (16), purple light lamp (16) are located the top of filter screen (15), purple light lamp (16) are located the bottom of purifying box (17), just equal fixed connection in filter screen (15) and purple light lamp (16) purifying box (17). (CN210945175)|TECHNICAL FIELD|[0002] The utility model belongs to the technical field of sewage treatment, especially, relate to a food sewage treatment plant with crushing function.|BACKGROUND ART|[0004] Recently, according to the increase of interest caused by environmental pollution caused by food waste, various technologies for an apparatus for food waste treatment have been proposed, and as an example, a food waste treatment apparatus in which a pressing unit presses food waste to remove water from the food waste is proposed to reduce odor emitted from the food waste and to reduce the weight of the food waste. The above-described conventional food waste treatment apparatus reduces environmental pollution and reduces food waste treatment costs by preventing odors emitted from relatively wet food waste because the food waste treatment apparatus removes water from the food waste.|[0005] When the sewage to food is handled in the existing market, the rubbish that mostly needs in the sewage to food is broken to collect the rubbish after the breakage, and the rubbish after the breakage can give off the peculiar smell equally, and then influences the follow-up processing of staff to rubbish.|DISCLOSURE|[0006] SUMMERY OF THE UTILITY MODEL|[0007] The utility model provides a food sewage treatment plant with crushing function, when aiming at solving the sewage to food on the existing market and handling, the most rubbish that need in the food sewage is broken to collect the rubbish after the breakage, and the rubbish after the breakage can distribute the peculiar smell equally, and then influences the follow-up processing problem of staff to rubbish.|[0008] The utility model discloses a realize like this, a food sewage treatment plant with crushing function, including broken subassembly and the subassembly of distinguishing flavor of, broken subassembly includes box, crushing roller, purifying box and breaker, the output transmission of breaker connect in the crushing roller, and be fixed in the inside of box, the purifying box is fixed in under the crushing roller, it includes fan, mounting panel and active carbon adsorption stick to distinguish flavor of, the through-hole has been seted up to the inside of box, active carbon adsorption stick accept in inside the through-hole, just the input and the output of fan all with the through-hole is linked together, and is fixed in the outer wall of box, just the mounting panel can be dismantled connect in the box, and with the mutual adaptation of through-hole.|[0009] Preferably, two openings are formed in the inner wall of the box body of the crushing roller, which is far away from the crusher, and the openings are communicated with the through hole.|[0010] Preferably, the number of the through holes is four, the four through holes surround the inside of the box body, and two ends of the through holes are respectively communicated with the two openings.|[0011] Preferably, the mounting plate is located the crushing roller is close to one side of breaker, just the active carbon adsorption stick centre gripping in the mounting plate with between the through-hole, and be located inside the through-hole that the mounting plate corresponds.|[0012] Preferably, the odor removing assembly further comprises two connecting pipes, the connecting pipes are fixed on the outer wall of the box body, the connecting pipes are hollow and penetrate through the outer wall of the box body, and the input end and the output end of the fan are fixedly connected to the connecting pipes through pipelines and communicated with the through holes through the connecting pipes.|[0013] Preferably, the fixed handle that is provided with of outer wall of mounting panel, just the handle is C shape, and be provided with the bull stick directly over the mounting panel, the bull stick rotate through the pivot connect in the outer wall of box, just the mounting panel passes through the bull stick joint in the box.|[0014] Preferably, the crushing assembly further comprises a blocking plate, a collecting box and a water discharging pipe, the blocking plate is fixed between the crushing roller and the purifying box, one end of the water discharging pipe is fixed on the purifying box and communicated with the inside of the purifying box, and the collecting box is located at the bottom of the box body and is connected to the box body in a sliding mode.|[0015] Preferably, the inside of purifying box is equipped with filter screen and purple light lamp, the purple light lamp is located the top of filter screen, the purple light lamp is located the bottom of purifying box, just equal fixed connection of filter screen and purple light lamp in purifying box.|[0016] Compared with the prior art, the beneficial effects of the utility model are that: the food sewage treatment device with the crushing function of the utility model is provided with the fan, the through hole, the active carbon adsorption rod and the mounting plate, in the using process, the air with peculiar smell in the box body can be pumped into the through hole by the fan, and flows along the through hole, and when the air passes through the active carbon adsorption rod, the peculiar smell in the air is removed by utilizing the adsorption of the active carbon, the treated air is continuously conveyed into the box body through the through holes, and then the air with peculiar smell is continuously pumped, purified and input, so that the peculiar smell in the box body can be continuously diluted, meanwhile, the installation plate can be taken down by the worker, and the activated carbon adsorption rod in the through hole is replaced, so that the subsequent odor removal can be smoothly carried out, and the peculiar smell in the box body is fully desalted, and the influence on the follow-up work of workers is avoided.|DRAWINGS DESCRIPTION|[0018] Fig. 1 is a schematic view of the internal structure of the present invention;|[0019] FIG. 2 is a schematic view of the through hole structure of the present invention;|[0020] fig. 3 is a schematic structural view of a fan in the present invention;|[0021] fig. 4 is a schematic view of the butt structure of the mounting plate in the present invention;|[0022] in the figure: 1. a crushing assembly; 11. a box body; 12. a crushing roller; 13. a blocking plate; 14. a collection box; 15. a filter screen; 16. an ultraviolet lamp; 17. a purification box; 18. a drain pipe; 19. a crusher; 2. a deodorizing component; 21. an opening; 22. a fan; 23. a rotating rod; 24. mounting a plate; 25. a handle; 26. a through hole; 27. an activated carbon adsorption rod; 28. the tube is connected.|INVENTION MODE|[0023] Detailed Description|[0024] In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.|[0025] Referring to fig. 1-4, the present invention provides a technical solution: the utility model provides a food sewage treatment plant with crushing function, include broken subassembly 1 and go flavor subassembly 2, broken subassembly 1 includes box 11, crushing roller 12, purifying box 17 and breaker 19, the output transmission of breaker 19 is connected in crushing roller 12, and be fixed in the inside of box 11, purifying box 17 is fixed in under the crushing roller 12, it includes fan 22 to go flavor subassembly 2, mounting panel 24 and active carbon adsorption stick 27, through-hole 26 has been seted up to the inside of box 11, active carbon adsorption stick 27 is acceptd inside through-hole 26, and fan 22's input and output all are linked together with through-hole 26, and be fixed in the outer wall of box 11, and mounting panel 24 can dismantle and connect in box 11, and with the mutual adaptation of through-hole 26.|[0026] In this embodiment, a crushing chamber is formed in the housing 11, the crushing roller 12 is accommodated in the crushing chamber, and food waste with sewage is crushed in the crushing chamber during use, and a spiral crushing blade is provided on the outer wall of the crushing roller 12 to crush and crush the food waste with the crushing blade, and one end of the crushing roller 12, which is far from the crusher 19, is tapered and provided with a raised grain converging toward one end of the crushing roller 12, so that the crushed food waste can be discharged from the crushing chamber and fall into the collecting box 14 by the grain.|[0027] In this embodiment, in the using process, the worker pours the food waste with the sewage into the inside from the feeding port of the box 11 and flows to the inside of the crushing chamber, then the crusher 19 starts to work and drives the crushing roller 12 to start to rotate, the waste is crushed by the rotation of the crushing roller 12, and the crushed waste can be discharged from the inside of the crushing chamber through one end of the crushing roller 12 and fall into the collecting box 14 at the bottom of the box 11, the crushed waste is stored and collected through the collecting box 14, secondly, the sewage entering the inside of the crushing chamber flows into the inside of the purifying box 17 through the baffle plate 13 and is filtered and sterilized through the filter screen 15 and the purple light lamp 16 inside the purifying box 17, and then the treated sewage is led to the outside through the drain pipe 18, and secondly, when the waste is over, the inside of the box 11 will contain a large amount of odor, at this time, the fan 22 starts to work, the fan 22 will flow the odor air inside the box 11 into the suction through hole 26 through one of the openings 21, and the odor air will be sucked into the through hole 26 and then discharged into the through hole 26 through the fan 22 again under the action of the fan 22, and then the ventilation speed of the odor air inside the through hole 26 will be increased under the action of the fan 22, because the activated carbon adsorption rod 27 is located inside the through hole 26, the odor air will contact with the activated carbon adsorption rod 27 during the ventilation process, and the odor in the air can be absorbed and removed by the adsorption of the activated carbon adsorption rod 27, and the odor in the air is reduced to content, and then the air after adsorption treatment can be discharged into the box 11 again through the other opening 21, and then continuously pumped, Purifying and inputting, the peculiar smell in the box body 11 can be continuously diluted, the influence on the subsequent work of the working personnel can be avoided, in addition, a certain distance is arranged between the two openings 21, the air after the adsorption treatment is prevented from being sucked into the through hole 26 again, after the activated carbon adsorption rod 27 is used for a certain time, the working personnel can rotate the rotating rod 23, so that one end of the rotating rod 23 is separated from the outer wall of the mounting plate 24, then, the working personnel can take out the mounting plate 24 through the handle 25, then, the activated carbon adsorption rod 27 in the through hole 26 can be replaced, then, the mounting plate 24 is mounted on the box body 11 again, the rotating rod 23 is rotated again, so that one end of the rotating rod 23 is lapped on the mounting plate 24, then, the mounting plate 24 can be fixed on the box body 11, and then, when the working personnel needs to treat the crushed garbage, as the bottom of the box body 11 is provided with the chute matched with the collecting box 14, the worker can pull the collecting box 14 to slide on the chute, so that the collecting box 14 can be taken out from the box body 11, and then the garbage collected in the collecting box 14 can be subjected to subsequent treatment.|[0028] Furthermore, two openings 21 are opened on the inner wall of the box 11 of the crushing roller 12 away from the crusher 19, and the openings 21 are communicated with the through hole 26.|[0029] In the present embodiment, during the use process, the two openings 21 are respectively used for exhausting the odor air and introducing the processed air, so that the air inside the box body 11 can be diluted continuously, and the influence on the normal work of the worker due to the odor is prevented.|[0030] Furthermore, the number of the through holes 26 is four, and the four through holes 26 surround the inside of the box body 11, and two ends of the through holes are respectively communicated with the two openings 21.|[0031] In the present embodiment, during the use of the pair, the connection between the through holes 26 and the opening 21 and the activated carbon adsorption rods 27 arranged inside each through hole 26 enable the odor air to be smoothly introduced into the through holes 26, and the odor in the air can be smoothly treated.|[0032] Further, the mounting plate 24 is located on the side of the crushing roller 12 close to the crusher 19, and the activated carbon adsorption rod 27 is sandwiched between the mounting plate 24 and the through hole 26 and located inside the through hole 26 corresponding to the mounting plate 24.|[0033] In the present embodiment, the position of the activated carbon adsorption rod 27 is set during use, so that the activated carbon adsorption rod 27 can be smoothly taken out after the mounting plate 24 is taken out, and the replacement of the activated carbon adsorption rod 27 can be smoothly completed.|[0034] Further, the odor removing assembly 2 further comprises two connecting pipes 28, the connecting pipes 28 are fixed on the outer wall of the box body 11, the two connecting pipes 28 are hollow and penetrate through the outer wall of the box body 11, and the input end and the output end of the fan 22 are fixedly connected to the connecting pipes 28 through pipelines and are communicated with the through holes 26 through the connecting pipes 28.|[0035] In the present embodiment, during the use process, the fan 22 can be smoothly communicated with the through hole 26 under the action of the connecting tube 28, the through hole 26 is divided into two sections, two ends of each section of the through hole 26 correspond to one connecting tube 28 and one opening 21, and the odor air can be smoothly introduced and treated.|[0036] Further, the outer wall of mounting panel 24 is fixed and is provided with handle 25, and handle 25 is C shape to be provided with bull stick 23 directly over mounting panel 24, bull stick 23 rotates through the pivot and connects in the outer wall of box 11, and mounting panel 24 passes through bull stick 23 joint in box 11.|[0037] In this embodiment, after the activated carbon adsorption rod 27 is replaced, the worker can mount the mounting plate 24 on the housing 11, rotate the rotary rod 23 so that one end of the rotary rod 23 is caught on the mounting plate 24, and fix the mounting plate 24 on the housing 11.|[0038] Further, crushing subassembly 1 still includes baffle 13, collecting box 14 and drain pipe 18, and baffle 13 is fixed in between crushing roller 12 and the purifying box 17, and the one end of drain pipe 18 is fixed in purifying box 17 to be linked together with the purifying box 17 is inside, and collecting box 14 is located the bottom of box 11, and sliding connection is in box 11.|[0039] In this embodiment, when the staff need handle the rubbish after smashing, owing to set up the spout with collecting box 14 looks adaptation in the bottom of box 11, and then the staff alright stimulate collecting box 14, make it slide on the spout, and then alright take out collecting box 14 from the inside of box 11, alright carry out subsequent processing to the rubbish of collecting 14 inside collection afterwards.|[0040] Further, the inside of purifying box 17 is equipped with filter screen 15 and purple light lamp 16, and purple light lamp 16 is located the top of filter screen 15, and purple light lamp 16 is located the bottom of purifying box 17, and filter screen 15 and the equal fixed connection of purple light lamp 16 in purifying box 17.|[0041] In this embodiment, during the use process, the sewage entering the crushing cavity flows into the purifying box 17 through the barrier 13, and is filtered and sterilized by the filter screen 15 and the ultraviolet lamp 16 inside the purifying box 17, and then the treated sewage is led to the outside through the drain pipe 18.|[0042] The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention. (CN210945175)|TECHNICAL FIELD|[0002] The utility model belongs to the technical field of sewage treatment, especially, relate to a food sewage treatment plant with crushing function.|BACKGROUND ART|[0004] Recently, according to the increase of interest caused by environmental pollution caused by food waste, various technologies for an apparatus for food waste treatment have been proposed, and as an example, a food waste treatment apparatus in which a pressing unit presses food waste to remove water from the food waste is proposed to reduce odor emitted from the food waste and to reduce the weight of the food waste. The above-described conventional food waste treatment apparatus reduces environmental pollution and reduces food waste treatment costs by preventing odors emitted from relatively wet food waste because the food waste treatment apparatus removes water from the food waste.|[0005] When the sewage to food is handled in the existing market, the rubbish that mostly needs in the sewage to food is broken to collect the rubbish after the breakage, and the rubbish after the breakage can give off the peculiar smell equally, and then influences the follow-up processing of staff to rubbish.|DISCLOSURE|[0006] SUMMERY OF THE UTILITY MODEL|[0007] The utility model provides a food sewage treatment plant with crushing function, when aiming at solving the sewage to food on the existing market and handling, the most rubbish that need in the food sewage is broken to collect the rubbish after the breakage, and the rubbish after the breakage can distribute the peculiar smell equally, and then influences the follow-up processing problem of staff to rubbish.|[0008] The utility model discloses a realize like this, a food sewage treatment plant with crushing function, including broken subassembly and the subassembly of distinguishing flavor of, broken subassembly includes box, crushing roller, purifying box and breaker, the output transmission of breaker connect in the crushing roller, and be fixed in the inside of box, the purifying box is fixed in under the crushing roller, it includes fan, mounting panel and active carbon adsorption stick to distinguish flavor of, the through-hole has been seted up to the inside of box, active carbon adsorption stick accept in inside the through-hole, just the input and the output of fan all with the through-hole is linked together, and is fixed in the outer wall of box, just the mounting panel can be dismantled connect in the box, and with the mutual adaptation of through-hole.|[0009] Preferably, two openings are formed in the inner wall of the box body of the crushing roller, which is far away from the crusher, and the openings are communicated with the through hole.|[0010] Preferably, the number of the through holes is four, the four through holes surround the inside of the box body, and two ends of the through holes are respectively communicated with the two openings.|[0011] Preferably, the mounting plate is located the crushing roller is close to one side of breaker, just the active carbon adsorption stick centre gripping in the mounting plate with between the through-hole, and be located inside the through-hole that the mounting plate corresponds.|[0012] Preferably, the odor removing assembly further comprises two connecting pipes, the connecting pipes are fixed on the outer wall of the box body, the connecting pipes are hollow and penetrate through the outer wall of the box body, and the input end and the output end of the fan are fixedly connected to the connecting pipes through pipelines and communicated with the through holes through the connecting pipes.|[0013] Preferably, the fixed handle that is provided with of outer wall of mounting panel, just the handle is C shape, and be provided with the bull stick directly over the mounting panel, the bull stick rotate through the pivot connect in the outer wall of box, just the mounting panel passes through the bull stick joint in the box.|[0014] Preferably, the crushing assembly further comprises a blocking plate, a collecting box and a water discharging pipe, the blocking plate is fixed between the crushing roller and the purifying box, one end of the water discharging pipe is fixed on the purifying box and communicated with the inside of the purifying box, and the collecting box is located at the bottom of the box body and is connected to the box body in a sliding mode.|[0015] Preferably, the inside of purifying box is equipped with filter screen and purple light lamp, the purple light lamp is located the top of filter screen, the purple light lamp is located the bottom of purifying box, just equal fixed connection of filter screen and purple light lamp in purifying box.|[0016] Compared with the prior art, the beneficial effects of the utility model are that: the food sewage treatment device with the crushing function of the utility model is provided with the fan, the through hole, the active carbon adsorption rod and the mounting plate, in the using process, the air with peculiar smell in the box body can be pumped into the through hole by the fan, and flows along the through hole, and when the air passes through the active carbon adsorption rod, the peculiar smell in the air is removed by utilizing the adsorption of the active carbon, the treated air is continuously conveyed into the box body through the through holes, and then the air with peculiar smell is continuously pumped, purified and input, so that the peculiar smell in the box body can be continuously diluted, meanwhile, the installation plate can be taken down by the worker, and the activated carbon adsorption rod in the through hole is replaced, so that the subsequent odor removal can be smoothly carried out, and the peculiar smell in the box body is fully desalted, and the influence on the follow-up work of workers is avoided.|DRAWINGS DESCRIPTION|[0018] Fig. 1 is a schematic view of the internal structure of the present invention;|[0019] FIG. 2 is a schematic view of the through hole structure of the present invention;|[0020] fig. 3 is a schematic structural view of a fan in the present invention;|[0021] fig. 4 is a schematic view of the butt structure of the mounting plate in the present invention;|[0022] in the figure: 1. a crushing assembly; 11. a box body; 12. a crushing roller; 13. a blocking plate; 14. a collection box; 15. a filter screen; 16. an ultraviolet lamp; 17. a purification box; 18. a drain pipe; 19. a crusher; 2. a deodorizing component; 21. an opening; 22. a fan; 23. a rotating rod; 24. mounting a plate; 25. a handle; 26. a through hole; 27. an activated carbon adsorption rod; 28. the tube is connected.|INVENTION MODE|[0023] Detailed Description|[0024] In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.|[0025] Referring to fig. 1-4, the present invention provides a technical solution: the utility model provides a food sewage treatment plant with crushing function, include broken subassembly 1 and go flavor subassembly 2, broken subassembly 1 includes box 11, crushing roller 12, purifying box 17 and breaker 19, the output transmission of breaker 19 is connected in crushing roller 12, and be fixed in the inside of box 11, purifying box 17 is fixed in under the crushing roller 12, it includes fan 22 to go flavor subassembly 2, mounting panel 24 and active carbon adsorption stick 27, through-hole 26 has been seted up to the inside of box 11, active carbon adsorption stick 27 is acceptd inside through-hole 26, and fan 22's input and output all are linked together with through-hole 26, and be fixed in the outer wall of box 11, and mounting panel 24 can dismantle and connect in box 11, and with the mutual adaptation of through-hole 26.|[0026] In this embodiment, a crushing chamber is formed in the housing 11, the crushing roller 12 is accommodated in the crushing chamber, and food waste with sewage is crushed in the crushing chamber during use, and a spiral crushing blade is provided on the outer wall of the crushing roller 12 to crush and crush the food waste with the crushing blade, and one end of the crushing roller 12, which is far from the crusher 19, is tapered and provided with a raised grain converging toward one end of the crushing roller 12, so that the crushed food waste can be discharged from the crushing chamber and fall into the collecting box 14 by the grain.|[0027] In this embodiment, in the using process, the worker pours the food waste with the sewage into the inside from the feeding port of the box 11 and flows to the inside of the crushing chamber, then the crusher 19 starts to work and drives the crushing roller 12 to start to rotate, the waste is crushed by the rotation of the crushing roller 12, and the crushed waste can be discharged from the inside of the crushing chamber through one end of the crushing roller 12 and fall into the collecting box 14 at the bottom of the box 11, the crushed waste is stored and collected through the collecting box 14, secondly, the sewage entering the inside of the crushing chamber flows into the inside of the purifying box 17 through the baffle plate 13 and is filtered and sterilized through the filter screen 15 and the purple light lamp 16 inside the purifying box 17, and then the treated sewage is led to the outside through the drain pipe 18, and secondly, when the waste is over, the inside of the box 11 will contain a large amount of odor, at this time, the fan 22 starts to work, the fan 22 will flow the odor air inside the box 11 into the suction through hole 26 through one of the openings 21, and the odor air will be sucked into the through hole 26 and then discharged into the through hole 26 through the fan 22 again under the action of the fan 22, and then the ventilation speed of the odor air inside the through hole 26 will be increased under the action of the fan 22, because the activated carbon adsorption rod 27 is located inside the through hole 26, the odor air will contact with the activated carbon adsorption rod 27 during the ventilation process, and the odor in the air can be absorbed and removed by the adsorption of the activated carbon adsorption rod 27, and the odor in the air is reduced to content, and then the air after adsorption treatment can be discharged into the box 11 again through the other opening 21, and then continuously pumped, Purifying and inputting, the peculiar smell in the box body 11 can be continuously diluted, the influence on the subsequent work of the working personnel can be avoided, in addition, a certain distance is arranged between the two openings 21, the air after the adsorption treatment is prevented from being sucked into the through hole 26 again, after the activated carbon adsorption rod 27 is used for a certain time, the working personnel can rotate the rotating rod 23, so that one end of the rotating rod 23 is separated from the outer wall of the mounting plate 24, then, the working personnel can take out the mounting plate 24 through the handle 25, then, the activated carbon adsorption rod 27 in the through hole 26 can be replaced, then, the mounting plate 24 is mounted on the box body 11 again, the rotating rod 23 is rotated again, so that one end of the rotating rod 23 is lapped on the mounting plate 24, then, the mounting plate 24 can be fixed on the box body 11, and then, when the working personnel needs to treat the crushed garbage, as the bottom of the box body 11 is provided with the chute matched with the collecting box 14, the worker can pull the collecting box 14 to slide on the chute, so that the collecting box 14 can be taken out from the box body 11, and then the garbage collected in the collecting box 14 can be subjected to subsequent treatment.|[0028] Furthermore, two openings 21 are opened on the inner wall of the box 11 of the crushing roller 12 away from the crusher 19, and the openings 21 are communicated with the through hole 26.|[0029] In the present embodiment, during the use process, the two openings 21 are respectively used for exhausting the odor air and introducing the processed air, so that the air inside the box body 11 can be diluted continuously, and the influence on the normal work of the worker due to the odor is prevented.|[0030] Furthermore, the number of the through holes 26 is four, and the four through holes 26 surround the inside of the box body 11, and two ends of the through holes are respectively communicated with the two openings 21.|[0031] In the present embodiment, during the use of the pair, the connection between the through holes 26 and the opening 21 and the activated carbon adsorption rods 27 arranged inside each through hole 26 enable the odor air to be smoothly introduced into the through holes 26, and the odor in the air can be smoothly treated.|[0032] Further, the mounting plate 24 is located on the side of the crushing roller 12 close to the crusher 19, and the activated carbon adsorption rod 27 is sandwiched between the mounting plate 24 and the through hole 26 and located inside the through hole 26 corresponding to the mounting plate 24.|[0033] In the present embodiment, the position of the activated carbon adsorption rod 27 is set during use, so that the activated carbon adsorption rod 27 can be smoothly taken out after the mounting plate 24 is taken out, and the replacement of the activated carbon adsorption rod 27 can be smoothly completed.|[0034] Further, the odor removing assembly 2 further comprises two connecting pipes 28, the connecting pipes 28 are fixed on the outer wall of the box body 11, the two connecting pipes 28 are hollow and penetrate through the outer wall of the box body 11, and the input end and the output end of the fan 22 are fixedly connected to the connecting pipes 28 through pipelines and are communicated with the through holes 26 through the connecting pipes 28.|[0035] In the present embodiment, during the use process, the fan 22 can be smoothly communicated with the through hole 26 under the action of the connecting tube 28, the through hole 26 is divided into two sections, two ends of each section of the through hole 26 correspond to one connecting tube 28 and one opening 21, and the odor air can be smoothly introduced and treated.|[0036] Further, the outer wall of mounting panel 24 is fixed and is provided with handle 25, and handle 25 is C shape to be provided with bull stick 23 directly over mounting panel 24, bull stick 23 rotates through the pivot and connects in the outer wall of box 11, and mounting panel 24 passes through bull stick 23 joint in box 11.|[0037] In this embodiment, after the activated carbon adsorption rod 27 is replaced, the worker can mount the mounting plate 24 on the housing 11, rotate the rotary rod 23 so that one end of the rotary rod 23 is caught on the mounting plate 24, and fix the mounting plate 24 on the housing 11.|[0038] Further, crushing subassembly 1 still includes baffle 13, collecting box 14 and drain pipe 18, and baffle 13 is fixed in between crushing roller 12 and the purifying box 17, and the one end of drain pipe 18 is fixed in purifying box 17 to be linked together with the purifying box 17 is inside, and collecting box 14 is located the bottom of box 11, and sliding connection is in box 11.|[0039] In this embodiment, when the staff need handle the rubbish after smashing, owing to set up the spout with collecting box 14 looks adaptation in the bottom of box 11, and then the staff alright stimulate collecting box 14, make it slide on the spout, and then alright take out collecting box 14 from the inside of box 11, alright carry out subsequent processing to the rubbish of collecting 14 inside collection afterwards.|[0040] Further, the inside of purifying box 17 is equipped with filter screen 15 and purple light lamp 16, and purple light lamp 16 is located the top of filter screen 15, and purple light lamp 16 is located the bottom of purifying box 17, and filter screen 15 and the equal fixed connection of purple light lamp 16 in purifying box 17.|[0041] In this embodiment, during the use process, the sewage entering the crushing cavity flows into the purifying box 17 through the barrier 13, and is filtered and sterilized by the filter screen 15 and the ultraviolet lamp 16 inside the purifying box 17, and then the treated sewage is led to the outside through the drain pipe 18.|[0042] The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention. Family Number|(89579289)|89579289|Abstract|(CN210945175U U)|The utility model is suitable for the technical field of sewage treatment . The food sewage treatment device with the crushing function comprises a crushing assembly and a deodorizing assembly , the crushing assembly comprises a box body , a crushing roller , a purifying box and a crusher , the output end of the crusher is in transmission connection with the crushing roller and is fixed in the box body , and the purifying box is fixed under the crushing roller ; air with peculiar smell in the box body can be pumped into the through hole through the fan ; flow along through holes , activated carbon adsorption rod , adsorption using activated carbon , removal of odors in air , the treated air is continuously conveyed into the box body through the through holes ; according to the air purification device , air with peculiar smell is continuously pumped , purified and input , so that the peculiar smell in the box body can be continuously desalted , and meanwhile , a worker can take down the mounting plate and replace the activated carbon adsorption rods in the through holes , so that subsequent peculiar smell removal can be smoothly carried out . |IPC codes|(CN210945175U U)|B01D - 053/04 |Title|(CN210945175U U)|Food sewage treatment device with crushing function | Chemical engineering|Environmental technology B01D-053/04|B02C-019/22|C02F-009/08 B01D-053/04|B02C-019/22|C02F-009/08 LAPSED (CN210945175)|LAPSED DEAD (CN210945175)|DEAD (CN210945175)|LEGAL DETAILS FOR CN210945175|Actual or expected expiration date=2021-09-18|Legal state=DEAD|Status=LAPSED|Event publication date=2019-09-18|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201921545593|Application date=2019-09-18|Standardized application number=2019CN-U1545593|Event publication date=2020-07-07|Event code=CN/U|Event indicator=Pos|Event group=Event indicating In Force|Registered Utility Model|Publication country=CN|Publication number=CN210945175|Publication stage code=U|Publication date=2020-07-07|Standardized publication number=CN210945175U|Event publication date=2020-07-07|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2022-08-26|Event code=CN/CF01|Event indicator=Neg|Event group=Event indicating Not In Force|Termination of patent right due to non-payment of annual fee|Effective date of the event=2021-09-18 https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=jf59U3ybGzYgi8xtVGDm2aqLeopS8oZMbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000043702174&ekey=2211&xpn=CN210945175U&kind=U https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=ihiH7IWaycG7QlbzIve9sLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN210945175)|CN (CN210945175)|NAME=NANTONG VOCATIONAL COLLEGE , COUNTRY=CN (CN210945175)|NAME=XU SIBO;BEIJING KEJIA INTELLECTUAL PROPERTY FIRM , REG=11427 (CN210945175)|NAME=ZHONG JIULONG|NAME=YANG LIJUN|NAME=DONG YANGQIN|NAME=SHU HUI 0 1 Titre: (CN210945175)|Food sewage treatment device with crushing function Résumé: (CN210945175)|The utility model is suitable for the technical field of sewage treatment. The food sewage treatment device with the crushing function comprises a crushing assembly and a deodorizing assembly, the crushing assembly comprises a box body, a crushing roller, a purifying box and a crusher, the output end of the crusher is in transmission connection with the crushing roller and is fixed in the box body, and the purifying box is fixed under the crushing roller; air with peculiar smell in the box body can be pumped into the through hole through the fan; flow along through holes, activated carbon adsorption rod, adsorption using activated carbon, removal of odors in air, the treated air is continuously conveyed into the box body through the through holes; according to the air purification device,air with peculiar smell is continuously pumped, purified and input, so that the peculiar smell in the box body can be continuously desalted, and meanwhile, a worker can take down the mounting plate and replace the activated carbon adsorption rods in the through holes, so that subsequent peculiar smell removal can be smoothly carried out. 58 Abstract gpt-4o-mini no The article focuses on a food sewage treatment device and odor removal, which does not relate to accelerated weathering or CO₂ capture.
58 IN202411102450 IN202411102450 IN202411102450 112975759 IN202411102450 A 2025-01-03 [IN202411102450] 2024-12-24 2024-12-24 2025-01-03 (IN202411102450)|2044-12-24 (IN202411102450)|A method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers (IN202411102450)|The present invention relates to a novel method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers derived from agricultural waste. The method comprises first treating the seeds with plasma for durations ranging from 0 to 10 seconds to improve seed germination in a soilless medium, and then incorporating the plasma-treated seeds into a soilless medium filled with agricultural biofertilizer. Integrating plasma treated seeds technology with a carbon rich biofertilizer derived from agricultural waste, using one of thermochemical processes, introduces a distinctive approach for sustainable agriculture. Unlike conventional methods, this method offers a multifaceted solution that addresses several critical aspects of modern agriculture, ranging from improved seed germination and plant growth to enhanced soil fertility and carbon sequestration. The seeds exposed to plasma for 8 seconds were sown on a soil-less medium and presented the highest germination percentage and seedling potency. The growth of both shoots and roots was improved as well. SEM, XRD, and FTIR, among other analytical techniques, were used to characterize plasma-treated seeds and biofertilizer incorporated into the soil-less growth medium. According to SEM images, there was a change in seed and biofertilizer morphology while FTIR and analyses showed certain alterations in functional group and chemistry of biofertilizer. Overall, this unique approach offers a scalable and adaptable solution for improving agricultural productivity. MANIPAL UNIVERSITY JAIPUR (IN202411102450)|MANIPAL UNIVERSITY JAIPUR Giri Rakhi|Ledwani Lalita|Sharma Abhishek (IN202411102450)|Giri Rakhi|Ledwani Lalita|Sharma Abhishek (IN202411102450)|The interpretation of these FTIR results gives necessary information on the chemical nature of groundnut shell biofertilizer, which helps to evaluate its possible uses such as soil improvement, or carbon sequestration.|The present invention method has the unique advantages over the conventional methods:- Using agricultural waste to create biofertilizers converts waste management issues into profitable resources.|However, their study did not explore the integration of this technology with biofertilizers, leaving a gap that this invention addresses.| (IN202411102450)|1. A method for enhancing seed productivity, comprising the following steps: Step 1: Treatment of seeds with plasma- - exposing the chili seeds to plasma at varying exposure times of 2, 4, 6, 8, and 10 seconds, at a distance of 3 cm from the treatment head; - generating a continuous arc at a frequency of 30-40 KHz to ionize the air and produce energized plasma; - applying the energized plasma to the surface of the seeds, thereby triggering the formation of free radicals on the treated surface; - promoting cross-linking between the water and the altered properties of the seed surface.. Step 2: Biofertilizer preparation- - collecting groundnut shell from farmlands and drying it in the sun to eliminate excess moisture; - feeding the dried groundnut shell into a hydraulic pellet press and pressing the shell into pellets using a horizontal die; - pyrolyzing the groundnut shell pellets in an auger reactor at a temperature of 500°C with a heating rate of 50°C/min to convert the pellets into biofertilizer; - grinding the resulting biofertilizer into fine crumbs and passing the crumbs through a 2 mm mesh to achieve a uniform particle size. Step 3: Preparing an aqueous extract of biofertilizer, - placing 1 gram of groundnut shell biofertilizer in a 100 mL Erlenmeyer flask; - adding 100 mL of distilled water to the flask; - shaking the flask for 2 hours at 120 rpm in the absence of light to prepare the biofertilizer extract. Step 4: Germination of the chilli seed - exposing the chili seeds to germination in a soilless medium and in the presence of groundnut shell biofertilizer; - Observing and comparing the germination rate and growth of the chili seeds in both conditions to assess the effects of the biofertilizer on seedling development.| (IN202411102450)|The present invention addresses the above-mentioned issues by integrating plasma-treated seed technology with a carbon-rich biofertilizer derived from agricultural waste.|The present invention relates to a novel method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers derived from agricultural waste.|The primary object of the present invention is to treat the seeds with plasma through ionized gas to enhance their quality, promoting faster and more uniform germination without chemicals.Another object of the present invention is to prepare the groundnut shell biofertilizer to maximize its efficiency and uniformity derived from agricultural waste, using one of thermochemical processes.The further object of the present invention is to provide a method for sustainable agriculture.| (IN202411102450)|BIOFERTILIZER(100,64)|PRODUCTIVITY(100,6)|INTEGRATING PLASMA TREATED SEED(100,4)|ENHANCING SEED PRODUCTIVITY(100,1)|CHILI SEED(58,14)|CHILI GERMINATION(57,2)|COLLECTING GROUNDNUT SHELL(57,2)|BIOFERTILIZER EXTRACT(51,12)|CHILI SEED GROWTH(50,3)|BIOFERTILIZER AQUEOUS EXTRACT(50,2)|PROFITABLE RESOURCE(50,1)|ENERGIZED PLASMA(45,5)|BIOFERTILIZER MORPHOLOGY(45,1)|CARBON RICH BIOFERTILIZER(43,3)|PROMOTING CROSSLINKING(43,2)|SOILLESS MEDIUM(41,6)|BIOFERTILIZER CHEMISTRY(41,1)|GROUNDNUT(40,12)|GROUNDNUT NATURE(39,1)|AGRICULTURAL BIOFERTILIZER(38,2)|CHILI SEED PLANT HEIGHT(38,1)|DRIED GROUNDNUT(37,2)|AGRICULTURAL WASTE(35,13)|UNIFORM GERMINATION(35,1)|AUGER REACTOR(33,4)|FINE CRUMB(32,2)|DEVELOPING SEEDLING(31,3)|PELLET(30,7)|CHILI(29,5)|PLASMA TREATMENT(28,21)|SUSTAINABLE AGRICULTURE(28,5)|AQUEOUS EXTRACT(28,2)|CHILI SEED SHOOT LENGTH(28,1)|SOIL FERTILITY ENHANCEMENT(27,1)|GERMINATION(26,8)|HYDRAULIC PELLET PRESS(26,2)|FLASK(25,4)|INTERPRETATION(25,1)|MULTIFACETED SOLUTION(25,1)|QUALITY ENHANCEMENT(25,1)|SCALABLE SOLUTION(25,1)|EXCESS MOISTURE(24,2)|CHILI SEED ROOT LENGTH(24,1)|AIR IONIZATION(23,2)|CRUMB(23,2)|SEED(22,13)|THERMOCHEMICAL(22,3)|FARMLAND(22,2)|HORIZONTAL DIE(22,2)|INTEGRATION(21,1)|ERLENMEYER FLASK(20,2)|ADAPTABLE SOLUTION(19,1)|CARBON SEQUESTRATION(17,4)|TREATMENT HEAD(17,3)|SHELL(17,2)|SUN(17,2)|WASTE MANAGEMENT(17,1)|SOIL IMPROVEMENT(14,1)|GERMINATION RATE(12,4)|SEED GERMINATION RATE(12,3)|DISTILLED WATER(11,27)|HEATING RATE(11,4)|BIOFERTILIZER RESULT(11,1)|GROUNDNUT MICROSCOPIC MORPHOLOGY(11,1)|FOURIER TRANSFORM INFRARED SPECTROSCOPY(10,6)|IONIZED GAS(9,2)|CHILI SEED MORPHOLOGY(9,1)|PLANT GROWTH(8,4)|STRETCHING VIBRATION(8,3)|PLASMA TREATED CHILI SEED(8,2)|UNIFORM PARTICLE SIZE(8,2)|CHILI SEED SEM ANALYSIS(8,1)|GERMINATING SEED COUNT(8,1)|GROUNDNUT CHARACTERIZATION(8,1)|GROWTH MEDIUM(8,1)|PLASMA TREATED CHILI GERMINATION(8,1)|SCANNING ELECTRON MICROSCOPE(7,8)|FREE RADICAL(7,3)|TREATED SURFACE(7,3)|BIOFERTILIZER NUTRIENT(7,1)|BIOFERTILIZER REACTIVITY(7,1)|GROUNDNUT DTA ANALYSIS(7,1)|SEED SURFACE(6,9)|GROUNDNUT ANALYSIS(6,2)|BIOFERTILIZER PELLET(6,1)|CARBON BIOFERTILIZER UTILIZATION(6,1)|CHILI SEED DEVELOPMENT(6,1)|HEALTHY SEEDLING(6,1)|HP CA 3D TREATER(6,1)|INNOVATIVE ALTERNATIVE(6,1)|NUTRIENT RICH BIOFERTILIZER(6,1)|NUTRIENT UPTAKE(6,1)|PLASMA TREATED SEED CHARACTERIZATION(6,1)|SUNFLOWER SEED ENHANCEMENT GROWTH(6,1)|UNTREATED SEED PLANT HEIGHT(6,1)|EXPERIMENT(5,4)|SOIL FERTILITY(5,3)|SHOOT LENGTH CHILI SEED(5,2)|BIOFERTILIZER EXTRACT TREATMENT(5,1)|ENVIRONMENT REHABILITATION(5,1)|FEEDSTOCK PELLET(5,1)|GERMINATION PROMOTING ENZYME(5,1)|HEALTHY BACTERIUM(5,1)|HELPFUL BACTERIUM(5,1)|HELPFUL MICROBE(5,1)|INSECT ATTACK(5,1)|MICROORGANISM HELP(5,1)|NUTRIENT DEPLETED SOILS(5,1)|PETRI DISH(5,1)|SEED STUDY(5,1)|SHOWCASE DURATION(5,1)|SOIL MICROBIOTA(5,1)|STANDARD 3D TREATER(5,1)|SUSTAINED PRODUCTIVITY(5,1)|UNCOVERED SEED(5,1)|INORGANIC GAS(4,2)|MAGNIFICATION(4,2)|AGRICULTURAL PRODUCTIVITY DECREASE(4,1)|ARC SPREADING ABILITY(4,1)|BIOFERTILIZER POTENTIAL(4,1)|BIOFERTILIZER SAMPLE(4,1)|BIOFERTILIZER TREATMENT(4,1)|CHILI PLANT(4,1)|CONVERTING TRASH(4,1)|DANGEROUS DISEASE(4,1)|DISPOSAL EXPENSE(4,1)|ENDOTHERMIC PEAK(4,1)|EXPOSING SEED(4,1)|FAST SPROUTING(4,1)|INTERNATIONAL SEED TESTING ASSOCIATION(4,1)|MOISTURE EVAPORATION(4,1)|NUMEROUS GERMINATION(4,1)|PEA SEED(4,1)|PLANT VIGOR(4,1)|PLASMA IONIZATION(4,1)|PLASMA THERAPY(4,1)|PLASMA TREATED SEED IMPACT(4,1)|RADICAL OCCURRENCE(4,1)|SEED ACTIVATION(4,1)|SEED PLASMA TREATMENT(4,1)|SEEDLING GROWTH(4,1)|SUSTAINABLE AGRICULTURAL PRACTICE(4,1)|SUSTAINABLE FARMING PRACTICE(4,1)|SYNERGISTIC BENEFIT(4,1)|UPTAKE POTENTIAL(4,1)|GROWN DISTILLED WATER(3,4)|ALIPHATIC HYDROCARBON(3,3)|DARK SETTING(3,1)|ECOSYSTEM(3,1)|ELECTRODE GEOMETRY(3,1)|ENOUGH NUTRIENT(3,1)|GERMINATION TEST(3,1)|GROWTH PARAMETER(3,1)|INCONSISTENCY(3,1)|ORGANIC DEBRIS(3,1)|PLASMA EXPOSURE(3,1)|PLASMA RADIATION(3,1)|REACTIVE SPECIES(3,1)|REGULAR MESH(3,1)|SOIL QUALITY DETERIORATION(3,1)|TREATMENT POST(3,1)|ULTRAHIGH VOLTAGE TRANSFORMER(3,1)|WASTE UTILIZATION(3,1)|AIR PLASMA TREATER(2,1)|ARC GENERATION FREQUENCY(2,1)|ATMOSPHERIC PLASMA TREATMENT(2,1)|BIODIVERSITY(2,1)|BRANCH(2,1)|BROAD PEAK(2,1)|CARBON HETEROATOM BOND(2,1)|COMPOST(2,1)|CROSSLINKING(2,1)| (IN202411102450)|1. A method for enhancing seed productivity, comprising the following steps: Step 1: Treatment of seeds with plasma- - exposing the chili seeds to plasma at varying exposure times of 2, 4, 6, 8, and 10 seconds, at a distance of 3 cm from the treatment head; - generating a continuous arc at a frequency of 30-40 KHz to ionize the air and produce energized plasma; - applying the energized plasma to the surface of the seeds, thereby triggering the formation of free radicals on the treated surface; - promoting cross-linking between the water and the altered properties of the seed surface.. Step 2: Biofertilizer preparation- - collecting groundnut shell from farmlands and drying it in the sun to eliminate excess moisture; - feeding the dried groundnut shell into a hydraulic pellet press and pressing the shell into pellets using a horizontal die; - pyrolyzing the groundnut shell pellets in an auger reactor at a temperature of 500°C with a heating rate of 50°C/min to convert the pellets into biofertilizer; - grinding the resulting biofertilizer into fine crumbs and passing the crumbs through a 2 mm mesh to achieve a uniform particle size. Step 3: Preparing an aqueous extract of biofertilizer, - placing 1 gram of groundnut shell biofertilizer in a 100 mL Erlenmeyer flask; - adding 100 mL of distilled water to the flask; - shaking the flask for 2 hours at 120 rpm in the absence of light to prepare the biofertilizer extract. Step 4: Germination of the chilli seed - exposing the chili seeds to germination in a soilless medium and in the presence of groundnut shell biofertilizer; - Observing and comparing the germination rate and growth of the chili seeds in both conditions to assess the effects of the biofertilizer on seedling development.|2. The method of enhancing seed productivity as claimed in the claim 1, wherein - Plasma treatment for 8 seconds with biofertilizer results in an astounding 96% seed germination rate, surpassing the 75% germination rate achieved with distilled water; - The root length of the chilli seeds after 8 sec of plasma treatment with ground nut shell bio fertiliser extracted is 8.25 cm, representing an increase of 106.25% compared to the root length of seeds treated with distilled water; - The shoot length of the chilli seeds after 4-second plasma treatment with biofertilizer extract resulted in a shoot length of 4.7 cm, showing an increase of 32-33% compared to the shoot length of seeds treated with distilled water; and - Plant height of the chilli seeds after 8-second plasma treatment with biofertilizer extract is 12.45 cm, showing an increase of 65-66% compared to the plant height of seeds treated with distilled water;|3. The method of enhancing seed productivity as claimed in the claim 1, wherein the biofertilizer is produced from agricultural waste. (IN202411102450)|Field of the Invention|The present invention belongs to the plasma seed treatment field, more particular to a method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers derived from agricultural waste.|Background of the Invention|The agricultural industry faces significant challenges, such as deteriorating soil quality, reduced crop yields, and the need for sustainable farming practices. Conventional farming methods often rely on chemical fertilizers, which can harm the environment, degrade soil quality, and diminish biodiversity. Additionally, seed germination and plant growth can be inconsistent, particularly in less-than-ideal conditions, resulting in decreased agricultural productivity.|Nantapan et al., (2019) demonstrated the atmospheric plasma treatment can modify seeds surface, enhancement growth of sunflower seeds. However, their study did not explore the integration of this technology with biofertilizers, leaving a gap that this invention addresses.|In related application, US Patent application no. US0005281315A (Krapivina, n.d.)describes a method for exposing seeds to a low-temperature gas plasma discharge in an inorganic gas or a mixture of inorganic gases. The plasma is generated at pressures ranging from 0.1 to 5 Torr, using oxygen, air, or oxygen-nitrogen mixtures, and the seeds are exposed for 5 to 300 seconds. The plasma is powered by a high-frequency generator operating at a frequency of 140 MHz, with a power density of 0.03 to 1.5 W/cm3. However, this method has a limited scope, as it focuses solely on plasma treatment and does not incorporate biofertilizers, which restricts its application in broader agricultural practices. Biofertilizers made from natural sources like compost, manure, and agricultural waste are high in necessary nutrients and helpful microbes. They improve soil fertility and plant development while lowering the use of synthetic fertilizers. Despite their benefits, biofertilizers alone may not always offer enough nutrients for optimal plant growth, especially in nutrient-depleted soils.|Cha et al., (2016) reviewed the production and utilization of carbon based biofertilizer.|Kwapinski et al., (2010) shows the potential of biofertilizer to improve soil fertility and crop yields. While biofertilizer has shown promise, the study did not explore its synergistic effects when combined with other seed enhancement technologies, which this invention leverages.|The present invention addresses the above-mentioned issues by integrating plasma-treated seed technology with a carbon-rich biofertilizer derived from agricultural waste. This integrated approach enhances seed germination, plant growth, soil fertility, and carbon sequestration, providing a comprehensive and long-lasting solution for modern agriculture.|Object of the present Invention|The primary object of the present invention is to treat the seeds with plasma through ionized gas to enhance their quality, promoting faster and more uniform germination without chemicals.|Another object of the present invention is to prepare the groundnut shell biofertilizer to maximize its efficiency and uniformity derived from agricultural waste, using one of thermochemical processes.|The further object of the present invention is to provide a method for sustainable agriculture.|Summary of the Invention|In accordance with an embodiment of the present invention, a method integrating plasma-treated seed technology with a carbon-rich biofertilizer derived from agricultural waste, using thermochemical processes, introduces a distinctive approach to sustainable agriculture. The method involves first treating the seeds with plasma for durations ranging from 0 to 10 seconds to improve seed germination in a soilless medium. Next, a biofertilizer is produced from agricultural waste-specifically groundnut shells (GNS)-which are compressed and pyrolyzed in an auger reactor at 500°C with a heating rate of 50°C/min. The resulting pellets are converted into biofertilizer. Finally, the plasma-treated seeds are incorporated into the soilless medium, which is filled with the agricultural biofertilizer." Seed germination and growth parameters were assessed as a function of treatments, including different durations of plasma exposure (2, 4, 6, 8, and 10 seconds). This controlled method provided insights into the potential synergistic effects of plasma and biofertilizer treatments on seedling development and agricultural productivity, aiming to optimize sustainable agricultural practices.|Brief Summary of the Figures|The illustrated embodiments of the subject matter will be understood by reference to the drawings, wherein like parts are designated by like numerals throughout. The following|description is intended only by way of example, and simply illustrates certain selected embodiments of devices, systems, and methods that are consistent with the subject matter as claimed herein, wherein:|Figure 1- a) Plasma apparatus (b) Seeds treated with plasma radiation|Figure 2 - (a) Auger reactor; (b) Ground nut shell feedstock pellets; (c) Ground nut shell biofertilizer pellets|Figure 3- Flow chart of overall process|Figure 4 - SEM analysis of Ground nut shell biofertilizer|Figure 5 - Chemical composition of ground nut shell biofertilizer|Figure 6 - FTIR analysis of ground nut shell biofertilizer|Figure 7 - TGA and DTA analysis of ground nut shell biofertilizer|Figure 8- Water uptake of different plasma treatment of seeds|Figure 9 - Sem analysis of Chilli seeds (A-control, B-2sec, C-4sec, D-6sec, E-8sec F-10sec) Figure 10- Germination percentage of plasma treated Chilli seeds grown distilled water and biofertilizer|Figure 11- Root Length of plasma treated chilli seeds grown distilled water and biofertilizer Figure 12- Shoot Length of plasma treated Chilli seeds grown distilled water and biofertilizer Figure 13- Plant Length of plasma treated Chilli seeds grown distilled water and biofertilizer Figure 14-(a) Plasma treated Chilli seeds with distilled water (b) Plasma treated Chilli seed with biofertilizer|Detailed Description of the Invention|The detailed description of various exemplary embodiments of the disclosure is described herein with reference to the accompanying drawings. It should be noted that the embodiments are described herein in such details as to clearly communicate the disclosure. However, the amount of details provided herein is not intended to limit the anticipated variations of embodiments; on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the scope of the present disclosure as defined by the appended claims.|It is also to be understood that various arrangements may be devised that, although not explicitly described or shown herein, embody the principles of the present disclosure. Moreover, all statements herein reciting principles, aspects, and embodiments of the present disclosure, as well as specific examples, are intended to encompass equivalents thereof.|The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments. As used herein, the singular forms "a"," "an" and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It will be further understood that the terms "comprises," "comprising," "includes" and/or "including," when used herein, specify the presence of stated features, integers, steps, operations, elements and/or components, but do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components and/or groups thereof.|The present invention represents a significant advancement in sustainable agriculture, featuring a novel combination of plasma-treated seeds and biofertilizer derived from agricultural waste.|In an embodiment, the present invention uniquely integrates plasma-treated seeds with biofertilizer made from agricultural waste, the method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers derived from agricultural waste includes:|Step 1: Treatment of seeds with plasma-|- exposing the chili seeds to plasma at varying exposure times of 2, 4, 6, 8, and 10 seconds, at a distance of 3 cm from the treatment head;|- generating a continuous arc at a frequency of 30-40 KHz to ionize the air and produce energized plasma;|- applying the energized plasma to the surface of the seeds, thereby triggering the formation of free radicals on the treated surface;|- promoting cross-linking between the water and the altered properties of the seed surface.|Step 2: Biofertilizer preparation-|- collecting groundnut shell from farmlands and drying it in the sun to eliminate excess moisture;|- feeding the dried groundnut shell into a hydraulic pellet press and pressing the shell into pellets using a horizontal die;|- pyrolyzing the groundnut shell pellets in an auger reactor at a temperature of 500°C with a heating rate of 50°C/min to convert the pellets into biofertilizer;|- grinding the resulting biofertilizer into fine crumbs and passing the crumbs through a 2 mm mesh to achieve a uniform particle size.|Step 3: Preparing an aqueous extract of biofertilizer,|- placing 1 gram of groundnut shell biofertilizer in a 100 mL Erlenmeyer flask;|- adding 100 mL of distilled water to the flask;|- shaking the flask for 2 hours at 120 rpm in the absence of light to prepare the biofertilizer extract.|Step 4: Germination of the chilli seed|- preparing 6 groups, each containing 40 chili seeds in different Petri dishes each;|- exposing the chili seeds to germination in a soilless medium and in the presence of groundnut shell biofertilizer;|- observing and comparing the germination rate and growth of the chili seeds in both conditions to assess the effects of the biofertilizer on seedling development.|One aspect of the present invention, Figure 1 shows a typical setup for an air plasma treater. This system comprises of two closely placed electrodes which are connected to the secondary winding of an ultra-high voltage transformer. Such a transformer changes the primary voltage to high voltage and regulates the current so that to maintain a continuous arc, which is sustained by a constant flow of air from either blower or compressed air. Arc generation frequency depends on treater type where HP and HP-CA 3D treaters generate 30-40 KHz and typical Standard 3D treaters yield the frequency equivalent to 50/60 Hz. Generation of continuous arc produces highly charged ionized plasma. When this energized plasma is applied to a seed surface it can trigger the formation of free radicals on the treated surface. This procedure promotes the cross-linking between the water and the seed surface's changed properties.|Several factors govern the spreading ability of the arc that includes the second voltage of the transformer, supplied air velocity, and electrode's geometry. The wider the arc, the higher the voltage and air velocity should be. However, exceeding the appropriate air velocity could prematurely disrupt the arc. In normal production set-up, the object surface should be placed about % inch (6mm) from the front treatment head. The shape of the treatment pattern on a standing object is oval and more or less close to the round one.|One aspect of the present invention, Plasma treatment includes exposing seeds to ionized gas (plasma), which alters the seed surface and increases water uptake. The plasma breaks down the physical barriers of the seed coat and activates germination-promoting enzymes. This treatment increases the seeds' metabolic processes, resulting in faster and more consistent germination. Enhanced water absorption and enzyme activation lead to faster sprouting and healthier seedlings.|Plasma treatment promotes root growth and branching, allowing plants to explore a bigger area of soil and gain more nutrients and water. Better root systems result in more effective nutrient uptake, aided by the nutrient-rich biofertilizer. Biofertilizers add helpful bacteria and fungi to the soil. These microorganisms help degrade organic debris, fix nitrogen, and compete with dangerous diseases.|The combination of plasma therapy and biofertilizer causes plants to use less synthetic fertilizer for optimal growth. This is because the biofertilizer's nutrients are used efficiently, and plasma-treated roots have a higher uptake potential.|Plasma-treated seeds produce healthier, more vigorous plants that are less susceptible to disease and insect attacks. Biofertilizers also encourage healthy bacteria that can combat diseases.|Improving plant health and soil microbiota reduces the need for chemical pesticides, further cutting costs and environmental effect.|Characterization of plasma treated seeds|A. Water Uptake|Different treatments were applied to each set of seeds with the respective weights recorded prior and post application of treatments. The seeds were placed in 100 ml of deionized water and allowed to imbibe for one day after treatment. The seeds were repeatedly removed from water at different time intervals (2, 4, 6, 12 and 24hr), dried on paper, and weighted immediately upon drying out of surfaces. To determine the water uptake percentage, the following equation, as provided, was utilized.|W % of water uptake = (Wafter-Wbefore)/ Wbefore X100|Figure 8 Soaking periods were used to determine water absorption in a 12-hour experiment for plasma treated chili seeds. The results showed progressive increase in upward water movement as the immersion time increased. Significant increase in water absorption of the seeds immersed for all 12 hours.|A comparison of plasma treatment times revealed that chili seeds treated with a 8-second plasma exhibited the most increased water uptake compared to those treated for 2, 4, 6 and the longest treatment time; namely a second. Moreover, chili plants treated with plasma for 8 s during the 12-hour soaking period showed a surprising increase in water absorption by 66.5% against the control group.|First, the present study of seeds after receiving treatment with plasma for 2, 4, 6 and 10 seconds showed improvements in water uptake reading as follows 50.96%, 51.6%, 53.63% and 59.3%.|B. Scanning electron microscope|SEM was used to examine the effects of different plasma treatments on seeds in this experiment. Throughout the study, there were six distinct plasma treatment groups with varying durations of exposure. They were: 2 seconds, 4 seconds, 6 seconds, 8 seconds, and 10 seconds. In addition, seeds that were left untreated were included in the control group.|The changes in morphology of Chilli seeds treated with plasma for various time periods, illustrated by SEM images at different magnifications presented on Figures 9 (A-F). In 2sec, 4 sec 6sec 8 sec and 10 sec and control the regular mesh like structure was observed. Therefore, these structures were highly compromised due to greater plasma exposure time because the seed surface morphology was altered significantly and tissue became more porous. Likewise for other studies, also in these experiments the probability of occurring more serious transformations on seed surface morphology increased with an extended time of plasma treatment. Hence, degree and size cracks depend upon a lengthy period to run into showcase duration. Since the cover of normal and uncovered seeds was completely different, changes in surface morphology of seed differed similarly. In the same way, such inconsistencies were found in etching of seed surfaces of barley and pea seed. They claimed that this may be related to the chemical reaction of CP reactive species with seed surface and different energy distribution of CP.|Characterisation of groundnut shell biofertilizer|A. Scanning Electron Microscope (SEM)|Figure 4 shows SEM microscopic morphology of groundnut shell-biofertilizer at 11,000 X and 3500 X magnifications. Porosity is characterized by a variety of holes of an irregular shape on the outer surface of the biofertilizer. The pores range from about 1.83 to 5.34 micrometeors in diameter. The surface looks rough with channels. Pores are evenly spaced out, but with different sizing and shape. It shows some larger interconnected pores which can be used for adsorption of gas and liquid. It has high carbon content because it is black in color. It also shows its large pores on the sides revealing how smooth or thin it is and the greater area of contact.|B. Energy-Dispersive X-ray Spectroscopy (EDX)|Fig.5 shows showed that biofertilizer consists of carbon, oxygen, and these elements were in the following rations, respectively: carbon - 75.1 %. Oxygen was 18.6% and Mg was 1.2%. Secondly, potassium (K), calcium (Ca) and sulphur (S) were present in trace amounts. Carbon predominates this clearly suggests that the groundnut shell biofertilizer can be used as fertilizer, in the rehabilitation of the environment and carbon sequestration. It is also because it is likely to improve soil quality and store carbon efficiently in different ecosystems.|C. Fourier-transform infrared spectroscopy (FTIR)|The FTIR analysis shows in figure 6 that groundnut shell biofertilizer exhibits several characteristic peaks and functional groups. The peak at 3849 cm-1 indicates hydroxyl groups like alcohols and phenols on biofertilizer's surface. These groups are also reactive and adsorbent and add to the reactivity of the biofertilizer. A broad peak at 3742 cm-1 attributed to C-H stretching vibrations, representative of aliphatic hydrocarbons. This peak at 3618 cm-1 may be from organic functional groups or aliphatic hydrocarbons. A number of C-H stretching vibrations associated with aliphatic hydrocarbon is observed at 2926 cm-1. The peak at 2359 cm-1 may be due to carbon-heteroatom bonds that make up biofertilizer. The peak at 1920 cm-1 indicates carbonyl groups pointing to C=O stretching vibration, which further analysis will identify the actual carbonyl functional groups. There is a typical aromatic ring peak at 1524 cm-1 seen characteristic to groundnut shells and other lignocellulosic materials. Another peak is observed for the biofertilizer at 1648 cm-1 signifying C=C stretching vibrations groups, which are indicative of aromatic rings, a common feature in lignocellulosic materials such as groundnut shells. At 1023 cm-1 there is a peak which may be linked C-O stretching vibrations suggesting the presence of oxygen containing functional groups such as ethers and esters. Finally, some peaks at 584 cm-1 and|525 cm-1 might also arise due to some specific structural features or impurities present in the biofertilizer.|The interpretation of these FTIR results gives necessary information on the chemical nature of groundnut shell biofertilizer, which helps to evaluate its possible uses such as soil improvement, or carbon sequestration.|D. TGA and DTA analysis|The TGA profiles in Figure 5 display data for different heating rates in the presence of nitrogen gas. The black lines indicate mass quantities at various temperatures, revealing three distinct stages of weight loss due to moisture and volatile organic components being lost from the groundnut shell biofertilizer samples. Initial mass loss occurs between 20-270°C, followed by significant weight loss due to burning fixed carbon between 250 and 500°C. The third stage, occurring between 500 and 800 degrees Celsius, is linked to the decomposition of lignin, which is relatively resistant when exposed to heat. DTA curves show endothermic peaks around 110°C indicating energy required for moisture evaporation from the samples. The carbonization process begins at approximately 400-500°C as indicated by minima hinting that it's an endothermic reaction.|Accordingly present invention mehod, Seeds germination test was conducted at petri dish with duplicates according to International Seed Testing Association procedures. Perform two set of experiments in one set 20 seeds are placed in 9cm diameter petri dish containing 5ml of distilled water on two layer of filter paper and other set of experiment containing 5ml of aqueous GNS biofertilizer. The present invention assessed the impact of plasma treated seeds with distilled water and plasma treated seeds with biofertilizer on seeds germination. The Petri dishes were kept in an incubator in darkness setting at a temperature of 25 degrees Celsius. Germination was defined as occurrence of a radical extending beyond the seed coat at its length of 2 mm. Count of the germinating seeds was taken 2-day interval for a period not exceeding 10 days. Estimation of many germination processes (germination %, root length and shoot length) of numerous germinations. Figure 5 shows a flow chart of overall process.|Effect of plasma and plasma with biofertilizer on germination|The present invention investigated the effects of different plasma treatments on chili seeds, along with the use of water and biofertilizer extract over 10 days. When the radical emerged to approximately 2 mm, seed germination was considered successful.|Figure 10 shows the results of treating chili seeds with plasma, either with distilled water or biofertilizer extract. The results show that biofertilizer extract significantly improves both seed germination rate and seedling growth when compared to distilled water. Plasma treatment of 8 seconds with biofertilizer resulted in an astounding 96% seed germination rate, surpassing the 75% germination rate achieved with distilled water, as seen and untreated seeds used as control 50% in distilled water and 85% in biofertilizer. This implies that the germination process is positively influenced by the application of biofertilizer extract during plasma treatment, demonstrating its potential as a helpful component in promoting the growth of chili seeds.|A. Root length|Table 1: Root length - chilli seed|Figure 11, In a plasma treatment of 8 seconds with biofertilizer extract, the root length reached 8.25 cm, while distilled water resulted in a root length of 4. At 2 seconds, 4 seconds, 6 seconds, and 10 seconds, the roots were 6.15 cm, 7.25 cm, 7.2 cm, and 5.5 cm, respectively. In contrast, untreated seeds showed root lengths of 3.55 cm, 4.1 cm, 3.2 cm, 4 cmand 3.5 cm for the same biofertilizer extract treatments. The seeds exhibited root lengths of 3.25 cm with biofertilizer and 3.05 cm with distilled water.|B. Shoot length|Table 2: Shoot length - chilli seed|The treating chili seeds with plasma had a significant impact on shoot length when combined with biofertilizer extract, compared to using distilled water or untreated seeds. The duration of the plasma treatment was also found to affect shoot length. Specifically, a 4-second plasma treatment with biofertilizer extract resulted in a shoot length of 4.7 cm, while using distilled water led to a shoot length of 3.55 cm. Additionally, at durations of 2 seconds, 6 seconds, 8 seconds, and 10 seconds of plasma treatment, the corresponding shoot lengths were measured at: - Biofertilizer Extract Treatment: 4.35 cm, 4.55 cm, 4.2cm and 4.5cm. Distilled water resulted in shoot lengths of 1.85 cm, 3.2 cm, 3.5 cm, and 2.6 cm for the respective biofertilizer extract treatments. Untreated seeds showed shoot lengths of 3 cm with biofertilizer and 1 cm with distilled water. This variation in shoot lengths suggests that the duration of plasma treatment can influence the growth and development of chili seeds. The presence of biofertilizer extract in the plasma-treated chili seeds may have contributed to the observed differences in shoot length. The results of this study suggest that biofertilizer extract, when combined with plasma treatment, can positively influence shoot length in chili seeds illustrated in figure 12|C. Plant Height|Table 3: Shoot length - chilli seed|Figure 13 represents the plan height of the plasma treated with biofertilizer extract chili seeds. This was compared to distilled water and untreated seeds. A variation in shoot length was evident with varying plasma treatment durations. The plant height increased to 12.45 cm with an 8-second plasma treatment using biofertilizer extract, compared to 7.5 cm with distilled water. Furthermore, the respective plant lengths were measured at 10.5 cm, 11.95 cm, 11.75 cm, and 10 cm after 2 seconds, 4 seconds, 6 seconds, and 10 seconds of plasma treatment, respectively. Alternatively, distilled water resulted in shoot lengths of 5.4 cm, 7.65 cm, 7.5 cm, and 5.95 cm for the corresponding biofertilizer extract treatments. The plant height of untreated seeds was 6.25 cm with biofertilizer, and 4.05 cm with distilled water.|The present invention method has the unique advantages over the conventional methods:|- Using agricultural waste to create biofertilizers converts waste management issues into profitable resources. This not only lowers disposal expenses, but also provides a cost-effective source of plant nutrients.|- This technique promotes circular economy principles by converting trash into useful inputs, which helps to improve overall sustainability.|- Plasma treatment requires less energy than typical seed treatments, making it more cost-effective. This efficiency lowers the total energy footprint of seed treatment processes.|- Efficient nutrient use and improved plant health eliminate the need for costly chemical fertilizers and pesticides, resulting in substantial cost savings for farmers.|- Biofertilizer use improves soil structure and fertility, resulting in long-term benefits such as reduced soil remediation and sustained productivity.|In conclusion, the novel combination of plasma-treated seeds and biofertilizer obtained from agricultural waste marks a big step forward in sustainable agriculture. The invention's distinguishing characteristics-non-chemical seed activation, waste utilization, synergistic benefits, environmental sustainability, economic advantages, and technological innovation- make it an innovative and effective option for increasing agricultural productivity and sustainability. This integrated strategy not only increases crop yields and quality, but it also promotes long-term soil health and decreases environmental impact, so creating a solid foundation for modern agricultural methods. (IN202411102450)|Field of the Invention|The present invention belongs to the plasma seed treatment field, more particular to a method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers derived from agricultural waste.|Background of the Invention|The agricultural industry faces significant challenges, such as deteriorating soil quality, reduced crop yields, and the need for sustainable farming practices. Conventional farming methods often rely on chemical fertilizers, which can harm the environment, degrade soil quality, and diminish biodiversity. Additionally, seed germination and plant growth can be inconsistent, particularly in less-than-ideal conditions, resulting in decreased agricultural productivity.|Nantapan et al., (2019) demonstrated the atmospheric plasma treatment can modify seeds surface, enhancement growth of sunflower seeds. However, their study did not explore the integration of this technology with biofertilizers, leaving a gap that this invention addresses.|In related application, US Patent application no. US0005281315A (Krapivina, n.d.)describes a method for exposing seeds to a low-temperature gas plasma discharge in an inorganic gas or a mixture of inorganic gases. The plasma is generated at pressures ranging from 0.1 to 5 Torr, using oxygen, air, or oxygen-nitrogen mixtures, and the seeds are exposed for 5 to 300 seconds. The plasma is powered by a high-frequency generator operating at a frequency of 140 MHz, with a power density of 0.03 to 1.5 W/cm3. However, this method has a limited scope, as it focuses solely on plasma treatment and does not incorporate biofertilizers, which restricts its application in broader agricultural practices. Biofertilizers made from natural sources like compost, manure, and agricultural waste are high in necessary nutrients and helpful microbes. They improve soil fertility and plant development while lowering the use of synthetic fertilizers. Despite their benefits, biofertilizers alone may not always offer enough nutrients for optimal plant growth, especially in nutrient-depleted soils.|Cha et al., (2016) reviewed the production and utilization of carbon based biofertilizer.|Kwapinski et al., (2010) shows the potential of biofertilizer to improve soil fertility and crop yields. While biofertilizer has shown promise, the study did not explore its synergistic effects when combined with other seed enhancement technologies, which this invention leverages.|The present invention addresses the above-mentioned issues by integrating plasma-treated seed technology with a carbon-rich biofertilizer derived from agricultural waste. This integrated approach enhances seed germination, plant growth, soil fertility, and carbon sequestration, providing a comprehensive and long-lasting solution for modern agriculture.|Object of the present Invention|The primary object of the present invention is to treat the seeds with plasma through ionized gas to enhance their quality, promoting faster and more uniform germination without chemicals.|Another object of the present invention is to prepare the groundnut shell biofertilizer to maximize its efficiency and uniformity derived from agricultural waste, using one of thermochemical processes.|The further object of the present invention is to provide a method for sustainable agriculture.|Summary of the Invention|In accordance with an embodiment of the present invention, a method integrating plasma-treated seed technology with a carbon-rich biofertilizer derived from agricultural waste, using thermochemical processes, introduces a distinctive approach to sustainable agriculture. The method involves first treating the seeds with plasma for durations ranging from 0 to 10 seconds to improve seed germination in a soilless medium. Next, a biofertilizer is produced from agricultural waste-specifically groundnut shells (GNS)-which are compressed and pyrolyzed in an auger reactor at 500°C with a heating rate of 50°C/min. The resulting pellets are converted into biofertilizer. Finally, the plasma-treated seeds are incorporated into the soilless medium, which is filled with the agricultural biofertilizer." Seed germination and growth parameters were assessed as a function of treatments, including different durations of plasma exposure (2, 4, 6, 8, and 10 seconds). This controlled method provided insights into the potential synergistic effects of plasma and biofertilizer treatments on seedling development and agricultural productivity, aiming to optimize sustainable agricultural practices.|Brief Summary of the Figures|The illustrated embodiments of the subject matter will be understood by reference to the drawings, wherein like parts are designated by like numerals throughout. The following|description is intended only by way of example, and simply illustrates certain selected embodiments of devices, systems, and methods that are consistent with the subject matter as claimed herein, wherein:|Figure 1- a) Plasma apparatus (b) Seeds treated with plasma radiation|Figure 2 - (a) Auger reactor; (b) Ground nut shell feedstock pellets; (c) Ground nut shell biofertilizer pellets|Figure 3- Flow chart of overall process|Figure 4 - SEM analysis of Ground nut shell biofertilizer|Figure 5 - Chemical composition of ground nut shell biofertilizer|Figure 6 - FTIR analysis of ground nut shell biofertilizer|Figure 7 - TGA and DTA analysis of ground nut shell biofertilizer|Figure 8- Water uptake of different plasma treatment of seeds|Figure 9 - Sem analysis of Chilli seeds (A-control, B-2sec, C-4sec, D-6sec, E-8sec F-10sec) Figure 10- Germination percentage of plasma treated Chilli seeds grown distilled water and biofertilizer|Figure 11- Root Length of plasma treated chilli seeds grown distilled water and biofertilizer Figure 12- Shoot Length of plasma treated Chilli seeds grown distilled water and biofertilizer Figure 13- Plant Length of plasma treated Chilli seeds grown distilled water and biofertilizer Figure 14-(a) Plasma treated Chilli seeds with distilled water (b) Plasma treated Chilli seed with biofertilizer|Detailed Description of the Invention|The detailed description of various exemplary embodiments of the disclosure is described herein with reference to the accompanying drawings. It should be noted that the embodiments are described herein in such details as to clearly communicate the disclosure. However, the amount of details provided herein is not intended to limit the anticipated variations of embodiments; on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the scope of the present disclosure as defined by the appended claims.|It is also to be understood that various arrangements may be devised that, although not explicitly described or shown herein, embody the principles of the present disclosure. Moreover, all statements herein reciting principles, aspects, and embodiments of the present disclosure, as well as specific examples, are intended to encompass equivalents thereof.|The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments. As used herein, the singular forms "a"," "an" and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It will be further understood that the terms "comprises," "comprising," "includes" and/or "including," when used herein, specify the presence of stated features, integers, steps, operations, elements and/or components, but do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components and/or groups thereof.|The present invention represents a significant advancement in sustainable agriculture, featuring a novel combination of plasma-treated seeds and biofertilizer derived from agricultural waste.|In an embodiment, the present invention uniquely integrates plasma-treated seeds with biofertilizer made from agricultural waste, the method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers derived from agricultural waste includes:|Step 1: Treatment of seeds with plasma-|- exposing the chili seeds to plasma at varying exposure times of 2, 4, 6, 8, and 10 seconds, at a distance of 3 cm from the treatment head;|- generating a continuous arc at a frequency of 30-40 KHz to ionize the air and produce energized plasma;|- applying the energized plasma to the surface of the seeds, thereby triggering the formation of free radicals on the treated surface;|- promoting cross-linking between the water and the altered properties of the seed surface.|Step 2: Biofertilizer preparation-|- collecting groundnut shell from farmlands and drying it in the sun to eliminate excess moisture;|- feeding the dried groundnut shell into a hydraulic pellet press and pressing the shell into pellets using a horizontal die;|- pyrolyzing the groundnut shell pellets in an auger reactor at a temperature of 500°C with a heating rate of 50°C/min to convert the pellets into biofertilizer;|- grinding the resulting biofertilizer into fine crumbs and passing the crumbs through a 2 mm mesh to achieve a uniform particle size.|Step 3: Preparing an aqueous extract of biofertilizer,|- placing 1 gram of groundnut shell biofertilizer in a 100 mL Erlenmeyer flask;|- adding 100 mL of distilled water to the flask;|- shaking the flask for 2 hours at 120 rpm in the absence of light to prepare the biofertilizer extract.|Step 4: Germination of the chilli seed|- preparing 6 groups, each containing 40 chili seeds in different Petri dishes each;|- exposing the chili seeds to germination in a soilless medium and in the presence of groundnut shell biofertilizer;|- observing and comparing the germination rate and growth of the chili seeds in both conditions to assess the effects of the biofertilizer on seedling development.|One aspect of the present invention, Figure 1 shows a typical setup for an air plasma treater. This system comprises of two closely placed electrodes which are connected to the secondary winding of an ultra-high voltage transformer. Such a transformer changes the primary voltage to high voltage and regulates the current so that to maintain a continuous arc, which is sustained by a constant flow of air from either blower or compressed air. Arc generation frequency depends on treater type where HP and HP-CA 3D treaters generate 30-40 KHz and typical Standard 3D treaters yield the frequency equivalent to 50/60 Hz. Generation of continuous arc produces highly charged ionized plasma. When this energized plasma is applied to a seed surface it can trigger the formation of free radicals on the treated surface. This procedure promotes the cross-linking between the water and the seed surface's changed properties.|Several factors govern the spreading ability of the arc that includes the second voltage of the transformer, supplied air velocity, and electrode's geometry. The wider the arc, the higher the voltage and air velocity should be. However, exceeding the appropriate air velocity could prematurely disrupt the arc. In normal production set-up, the object surface should be placed about % inch (6mm) from the front treatment head. The shape of the treatment pattern on a standing object is oval and more or less close to the round one.|One aspect of the present invention, Plasma treatment includes exposing seeds to ionized gas (plasma), which alters the seed surface and increases water uptake. The plasma breaks down the physical barriers of the seed coat and activates germination-promoting enzymes. This treatment increases the seeds' metabolic processes, resulting in faster and more consistent germination. Enhanced water absorption and enzyme activation lead to faster sprouting and healthier seedlings.|Plasma treatment promotes root growth and branching, allowing plants to explore a bigger area of soil and gain more nutrients and water. Better root systems result in more effective nutrient uptake, aided by the nutrient-rich biofertilizer. Biofertilizers add helpful bacteria and fungi to the soil. These microorganisms help degrade organic debris, fix nitrogen, and compete with dangerous diseases.|The combination of plasma therapy and biofertilizer causes plants to use less synthetic fertilizer for optimal growth. This is because the biofertilizer's nutrients are used efficiently, and plasma-treated roots have a higher uptake potential.|Plasma-treated seeds produce healthier, more vigorous plants that are less susceptible to disease and insect attacks. Biofertilizers also encourage healthy bacteria that can combat diseases.|Improving plant health and soil microbiota reduces the need for chemical pesticides, further cutting costs and environmental effect.|Characterization of plasma treated seeds|A. Water Uptake|Different treatments were applied to each set of seeds with the respective weights recorded prior and post application of treatments. The seeds were placed in 100 ml of deionized water and allowed to imbibe for one day after treatment. The seeds were repeatedly removed from water at different time intervals (2, 4, 6, 12 and 24hr), dried on paper, and weighted immediately upon drying out of surfaces. To determine the water uptake percentage, the following equation, as provided, was utilized.|W % of water uptake = (Wafter-Wbefore)/ Wbefore X100|Figure 8 Soaking periods were used to determine water absorption in a 12-hour experiment for plasma treated chili seeds. The results showed progressive increase in upward water movement as the immersion time increased. Significant increase in water absorption of the seeds immersed for all 12 hours.|A comparison of plasma treatment times revealed that chili seeds treated with a 8-second plasma exhibited the most increased water uptake compared to those treated for 2, 4, 6 and the longest treatment time; namely a second. Moreover, chili plants treated with plasma for 8 s during the 12-hour soaking period showed a surprising increase in water absorption by 66.5% against the control group.|First, the present study of seeds after receiving treatment with plasma for 2, 4, 6 and 10 seconds showed improvements in water uptake reading as follows 50.96%, 51.6%, 53.63% and 59.3%.|B. Scanning electron microscope|SEM was used to examine the effects of different plasma treatments on seeds in this experiment. Throughout the study, there were six distinct plasma treatment groups with varying durations of exposure. They were: 2 seconds, 4 seconds, 6 seconds, 8 seconds, and 10 seconds. In addition, seeds that were left untreated were included in the control group.|The changes in morphology of Chilli seeds treated with plasma for various time periods, illustrated by SEM images at different magnifications presented on Figures 9 (A-F). In 2sec, 4 sec 6sec 8 sec and 10 sec and control the regular mesh like structure was observed. Therefore, these structures were highly compromised due to greater plasma exposure time because the seed surface morphology was altered significantly and tissue became more porous. Likewise for other studies, also in these experiments the probability of occurring more serious transformations on seed surface morphology increased with an extended time of plasma treatment. Hence, degree and size cracks depend upon a lengthy period to run into showcase duration. Since the cover of normal and uncovered seeds was completely different, changes in surface morphology of seed differed similarly. In the same way, such inconsistencies were found in etching of seed surfaces of barley and pea seed. They claimed that this may be related to the chemical reaction of CP reactive species with seed surface and different energy distribution of CP.|Characterisation of groundnut shell biofertilizer|A. Scanning Electron Microscope (SEM)|Figure 4 shows SEM microscopic morphology of groundnut shell-biofertilizer at 11,000 X and 3500 X magnifications. Porosity is characterized by a variety of holes of an irregular shape on the outer surface of the biofertilizer. The pores range from about 1.83 to 5.34 micrometeors in diameter. The surface looks rough with channels. Pores are evenly spaced out, but with different sizing and shape. It shows some larger interconnected pores which can be used for adsorption of gas and liquid. It has high carbon content because it is black in color. It also shows its large pores on the sides revealing how smooth or thin it is and the greater area of contact.|B. Energy-Dispersive X-ray Spectroscopy (EDX)|Fig.5 shows showed that biofertilizer consists of carbon, oxygen, and these elements were in the following rations, respectively: carbon - 75.1 %. Oxygen was 18.6% and Mg was 1.2%. Secondly, potassium (K), calcium (Ca) and sulphur (S) were present in trace amounts. Carbon predominates this clearly suggests that the groundnut shell biofertilizer can be used as fertilizer, in the rehabilitation of the environment and carbon sequestration. It is also because it is likely to improve soil quality and store carbon efficiently in different ecosystems.|C. Fourier-transform infrared spectroscopy (FTIR)|The FTIR analysis shows in figure 6 that groundnut shell biofertilizer exhibits several characteristic peaks and functional groups. The peak at 3849 cm-1 indicates hydroxyl groups like alcohols and phenols on biofertilizer's surface. These groups are also reactive and adsorbent and add to the reactivity of the biofertilizer. A broad peak at 3742 cm-1 attributed to C-H stretching vibrations, representative of aliphatic hydrocarbons. This peak at 3618 cm-1 may be from organic functional groups or aliphatic hydrocarbons. A number of C-H stretching vibrations associated with aliphatic hydrocarbon is observed at 2926 cm-1. The peak at 2359 cm-1 may be due to carbon-heteroatom bonds that make up biofertilizer. The peak at 1920 cm-1 indicates carbonyl groups pointing to C=O stretching vibration, which further analysis will identify the actual carbonyl functional groups. There is a typical aromatic ring peak at 1524 cm-1 seen characteristic to groundnut shells and other lignocellulosic materials. Another peak is observed for the biofertilizer at 1648 cm-1 signifying C=C stretching vibrations groups, which are indicative of aromatic rings, a common feature in lignocellulosic materials such as groundnut shells. At 1023 cm-1 there is a peak which may be linked C-O stretching vibrations suggesting the presence of oxygen containing functional groups such as ethers and esters. Finally, some peaks at 584 cm-1 and|525 cm-1 might also arise due to some specific structural features or impurities present in the biofertilizer.|The interpretation of these FTIR results gives necessary information on the chemical nature of groundnut shell biofertilizer, which helps to evaluate its possible uses such as soil improvement, or carbon sequestration.|D. TGA and DTA analysis|The TGA profiles in Figure 5 display data for different heating rates in the presence of nitrogen gas. The black lines indicate mass quantities at various temperatures, revealing three distinct stages of weight loss due to moisture and volatile organic components being lost from the groundnut shell biofertilizer samples. Initial mass loss occurs between 20-270°C, followed by significant weight loss due to burning fixed carbon between 250 and 500°C. The third stage, occurring between 500 and 800 degrees Celsius, is linked to the decomposition of lignin, which is relatively resistant when exposed to heat. DTA curves show endothermic peaks around 110°C indicating energy required for moisture evaporation from the samples. The carbonization process begins at approximately 400-500°C as indicated by minima hinting that it's an endothermic reaction.|Accordingly present invention mehod, Seeds germination test was conducted at petri dish with duplicates according to International Seed Testing Association procedures. Perform two set of experiments in one set 20 seeds are placed in 9cm diameter petri dish containing 5ml of distilled water on two layer of filter paper and other set of experiment containing 5ml of aqueous GNS biofertilizer. The present invention assessed the impact of plasma treated seeds with distilled water and plasma treated seeds with biofertilizer on seeds germination. The Petri dishes were kept in an incubator in darkness setting at a temperature of 25 degrees Celsius. Germination was defined as occurrence of a radical extending beyond the seed coat at its length of 2 mm. Count of the germinating seeds was taken 2-day interval for a period not exceeding 10 days. Estimation of many germination processes (germination %, root length and shoot length) of numerous germinations. Figure 5 shows a flow chart of overall process.|Effect of plasma and plasma with biofertilizer on germination|The present invention investigated the effects of different plasma treatments on chili seeds, along with the use of water and biofertilizer extract over 10 days. When the radical emerged to approximately 2 mm, seed germination was considered successful.|Figure 10 shows the results of treating chili seeds with plasma, either with distilled water or biofertilizer extract. The results show that biofertilizer extract significantly improves both seed germination rate and seedling growth when compared to distilled water. Plasma treatment of 8 seconds with biofertilizer resulted in an astounding 96% seed germination rate, surpassing the 75% germination rate achieved with distilled water, as seen and untreated seeds used as control 50% in distilled water and 85% in biofertilizer. This implies that the germination process is positively influenced by the application of biofertilizer extract during plasma treatment, demonstrating its potential as a helpful component in promoting the growth of chili seeds.|A. Root length|Table 1: Root length - chilli seed|Figure 11, In a plasma treatment of 8 seconds with biofertilizer extract, the root length reached 8.25 cm, while distilled water resulted in a root length of 4. At 2 seconds, 4 seconds, 6 seconds, and 10 seconds, the roots were 6.15 cm, 7.25 cm, 7.2 cm, and 5.5 cm, respectively. In contrast, untreated seeds showed root lengths of 3.55 cm, 4.1 cm, 3.2 cm, 4 cmand 3.5 cm for the same biofertilizer extract treatments. The seeds exhibited root lengths of 3.25 cm with biofertilizer and 3.05 cm with distilled water.|B. Shoot length|Table 2: Shoot length - chilli seed|The treating chili seeds with plasma had a significant impact on shoot length when combined with biofertilizer extract, compared to using distilled water or untreated seeds. The duration of the plasma treatment was also found to affect shoot length. Specifically, a 4-second plasma treatment with biofertilizer extract resulted in a shoot length of 4.7 cm, while using distilled water led to a shoot length of 3.55 cm. Additionally, at durations of 2 seconds, 6 seconds, 8 seconds, and 10 seconds of plasma treatment, the corresponding shoot lengths were measured at: - Biofertilizer Extract Treatment: 4.35 cm, 4.55 cm, 4.2cm and 4.5cm. Distilled water resulted in shoot lengths of 1.85 cm, 3.2 cm, 3.5 cm, and 2.6 cm for the respective biofertilizer extract treatments. Untreated seeds showed shoot lengths of 3 cm with biofertilizer and 1 cm with distilled water. This variation in shoot lengths suggests that the duration of plasma treatment can influence the growth and development of chili seeds. The presence of biofertilizer extract in the plasma-treated chili seeds may have contributed to the observed differences in shoot length. The results of this study suggest that biofertilizer extract, when combined with plasma treatment, can positively influence shoot length in chili seeds illustrated in figure 12|C. Plant Height|Table 3: Shoot length - chilli seed|Figure 13 represents the plan height of the plasma treated with biofertilizer extract chili seeds. This was compared to distilled water and untreated seeds. A variation in shoot length was evident with varying plasma treatment durations. The plant height increased to 12.45 cm with an 8-second plasma treatment using biofertilizer extract, compared to 7.5 cm with distilled water. Furthermore, the respective plant lengths were measured at 10.5 cm, 11.95 cm, 11.75 cm, and 10 cm after 2 seconds, 4 seconds, 6 seconds, and 10 seconds of plasma treatment, respectively. Alternatively, distilled water resulted in shoot lengths of 5.4 cm, 7.65 cm, 7.5 cm, and 5.95 cm for the corresponding biofertilizer extract treatments. The plant height of untreated seeds was 6.25 cm with biofertilizer, and 4.05 cm with distilled water.|The present invention method has the unique advantages over the conventional methods:|- Using agricultural waste to create biofertilizers converts waste management issues into profitable resources. This not only lowers disposal expenses, but also provides a cost-effective source of plant nutrients.|- This technique promotes circular economy principles by converting trash into useful inputs, which helps to improve overall sustainability.|- Plasma treatment requires less energy than typical seed treatments, making it more cost-effective. This efficiency lowers the total energy footprint of seed treatment processes.|- Efficient nutrient use and improved plant health eliminate the need for costly chemical fertilizers and pesticides, resulting in substantial cost savings for farmers.|- Biofertilizer use improves soil structure and fertility, resulting in long-term benefits such as reduced soil remediation and sustained productivity.|In conclusion, the novel combination of plasma-treated seeds and biofertilizer obtained from agricultural waste marks a big step forward in sustainable agriculture. The invention's distinguishing characteristics-non-chemical seed activation, waste utilization, synergistic benefits, environmental sustainability, economic advantages, and technological innovation- make it an innovative and effective option for increasing agricultural productivity and sustainability. This integrated strategy not only increases crop yields and quality, but it also promotes long-term soil health and decreases environmental impact, so creating a solid foundation for modern agricultural methods. Family Number|(112975759)|112975759|Abstract|(IN202411102450 A)|The present invention relates to a novel method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers derived from agricultural waste. The method comprises first treating the seeds with plasma for durations ranging from 0 to 10 seconds to improve seed germination in a soilless medium, and then incorporating the plasma-treated seeds into a soilless medium filled with agricultural biofertilizer. Integrating plasma treated seeds technology with a carbon rich biofertilizer derived from agricultural waste, using one of thermochemical processes, introduces a distinctive approach for sustainable agriculture. Unlike conventional methods, this method offers a multifaceted solution that addresses several critical aspects of modern agriculture, ranging from improved seed germination and plant growth to enhanced soil fertility and carbon sequestration. The seeds exposed to plasma for 8 seconds were sown on a soil-less medium and presented the highest germination percentage and seedling potency. The growth of both shoots and roots was improved as well. SEM, XRD, and FTIR, among other analytical techniques, were used to characterize plasma-treated seeds and biofertilizer incorporated into the soil-less growth medium. According to SEM images, there was a change in seed and biofertilizer morphology while FTIR and analyses showed certain alterations in functional group and chemistry of biofertilizer. Overall, this unique approach offers a scalable and adaptable solution for improving agricultural productivity.|IPC codes|(IN202411102450 A)|A01C-001/02|A01G-031/00|A01H-003/00|G01N-021/35| Basic materials chemistry|Food chemistry|Measurement|Other special machines A01C-001/02|A01G-031/00|A01H-003/00|C05F-011/08|G01N-021/35 A01C-001/02|A01G-031/00|A01H-003/00|C05F-011/08|G01N-021/35 PENDING (IN202411102450)|PENDING ALIVE (IN202411102450)|ALIVE (IN202411102450)|LEGAL DETAILS FOR IN202411102450|Actual or expected expiration date=2044-12-24|Legal state=ALIVE|Status=PENDING|Event publication date=2024-12-24|Event code=IN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=IN IN202411102450|Application date=2024-12-24|Standardized application number=2024IN-11102450|Event publication date=2025-01-03|Event code=IN/A|Event indicator=Pos|Event group=Examination events|Application laid open|Publication country=IN|Publication number=IN202411102450|Publication stage code=A|Publication date=2025-01-03|Standardized publication number=IN202411102450 (IN202411102450)|IN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=/WizbbSQlgsDAH62P6rL++Zy1L03KekLa/WZFbsCsqzB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=IN0000000001579532&ekey=2276&xpn=IN202411102450&kind=A https://iprsearch.ipindia.gov.in/PublicSearch/PublicationSearch/ApplicationStatus https://permalink.orbit.com/RenderStaticFirstPage?XPN=BR8IoTVlkae1OSxZSZBWzMExnvIz5kLrfqHome9U%252B8A%3D%26n%3D1&id=0&base=FAMPAT IN (IN202411102450)|NAME=Giri Rakhi|NAME=Ledwani Lalita|NAME=Sharma Abhishek 0 1 Titre: (IN202411102450)|A method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers Résumé: (IN202411102450)|The present invention relates to a novel method for enhancing seed productivity by integrating plasma-treated seeds with biofertilizers derived from agricultural waste. The method comprises first treating the seeds with plasma for durations ranging from 0 to 10 seconds to improve seed germination in a soilless medium, and then incorporating the plasma-treated seeds into a soilless medium filled with agricultural biofertilizer. Integrating plasma treated seeds technology with a carbon rich biofertilizer derived from agricultural waste, using one of thermochemical processes, introduces a distinctive approach for sustainable agriculture. Unlike conventional methods, this method offers a multifaceted solution that addresses several critical aspects of modern agriculture, ranging from improved seed germination and plant growth to enhanced soil fertility and carbon sequestration. The seeds exposed to plasma for 8 seconds were sown on a soil-less medium and presented the highest germination percentage and seedling potency. The growth of both shoots and roots was improved as well. SEM, XRD, and FTIR, among other analytical techniques, were used to characterize plasma-treated seeds and biofertilizer incorporated into the soil-less growth medium. According to SEM images, there was a change in seed and biofertilizer morphology while FTIR and analyses showed certain alterations in functional group and chemistry of biofertilizer. Overall, this unique approach offers a scalable and adaptable solution for improving agricultural productivity. 52 Abstract gpt-4o-mini no The article focuses on enhancing seed productivity and soil fertility through plasma-treated seeds and biofertilizers, without a clear connection to accelerated weathering or CO₂ capture.
59 CN202020841099U CN202020841099U CN212549743 92807669 CN212549743 U 2021-02-19 [CN212549743U] 2020-05-19 2020-05-19 2021-02-19 (CN212549743U)|2021-02-19 (CN212549743)|2023-05-23 (CN212549743)|Crushing device for hydraulic engineering construction (CN212549743)|The utility model relates to the technical field of water conservancy project construction, and discloses a crushing device for water conservancy project construction, which comprises a crushing box,crushing rollers are movably connected to the left end and the right end of an inner cavity of the crushing box, a dust removal box is fixedly connected to the top of the crushing box, and a filter screen is fixedly connected to the bottom of the inner cavity of the crushing box. A dust removal fan is fixedly connected to the position, located in the dust removal box, of the top of the crushing box, a sealing plate is movably connected to the top of the dust removal box through bolts, pressing rods are fixedly connected to the left end and the right end of the bottom of the sealing plate, andthe bottoms of the pressing rods abut against sliding blocks; an activated carbon dust removal plate is fixedly connected between the opposite sides of the two sliding blocks. According to the crushing device for hydraulic engineering construction, when materials are crushed, dust is removed, the surrounding environment is protected, meanwhile, the health of workers is guaranteed, the activated carbon dust removal plate is convenient to disassemble and assemble, the service life of the activated carbon dust removal plate is prolonged, and the crushing device is suitable for various conditions. LUO SHAOFENG ([CN]) (CN212549743)|LUO SHAOFENG ([CN]) LUO SHAOFENG (CN212549743)|LUO SHAOFENG (CN212549743)|CAO YUQING;BEIJING JINCHUANG INTELLECTUAL PROPERTY AGENCY FIRM|Reg. Nb: 11589 (CN212549743)|Along with the development of science and technology, hydraulic engineering construction has become an independent subject, and the current breaker for hydraulic engineering construction in the market at present does not have the shortcoming of removing dust, and when using, breaker to the broken in-process of soil stone, can produce a large amount of dusts, and the dust is directly discharged into the air, has not only polluted the surrounding environment, has damaged staff's health simultaneously, so proposes above-mentioned breaker for hydraulic engineering construction in order to solve above-mentioned problem.| (CN212549743)|1. The utility model provides a breaker for hydraulic engineering construction, includes broken case (1), its characterized in that: the dust removing device is characterized in that the left end and the right end of an inner cavity of the crushing box (1) are respectively and movably connected with a crushing roller (2), the top of the crushing box (1) is fixedly connected with a dust removing box (3), the bottom of the inner cavity of the crushing box (1) is fixedly connected with a filter screen (4), the top of the crushing box (1) is positioned in the dust removing box (3) and is fixedly connected with a dust removing fan (5), the top of the dust removing box (3) is movably connected with a sealing plate (6) through a bolt, the left end and the right end of the bottom of the sealing plate (6) are respectively and fixedly connected with a pressure lever (7), the bottom of the pressure lever (7) is abutted with a sliding block (8), two opposite sides of the sliding block (8) are respectively and fixedly connected with an active carbon dust removing plate (9), the left bottom of the crushing box (1, the positive right side swing joint of eccentric wheel (11) has connecting rod (12), the right side of connecting rod (12) articulates there is screen cloth (13), the left side of screen cloth (13) bottom articulates there is bracing piece (14), the right side fixedly connected with guide plate (15) of broken case (1) inner chamber bottom, the right side fixedly connected with screw conveyer (16) of broken case (1), the top fixedly connected with lifting motor (18) of screw conveyer (16), the output shaft fixedly connected with screw axis (17) of lifting motor (18), the positive top intercommunication of screw conveyer (16) has connecting pipe (19), the positive top intercommunication of broken case (1) has inlet pipe (20).| (CN212549743)|The utility model relates to a hydraulic engineering construction technical field just discloses a breaker is used in hydraulic engineering construction, including broken case, the equal swing joint in both ends has the crushing roller about broken incasement chamber, the top fixedly connected with dust removal case of broken case, the bottom fixedly connected with filter screen of broken incasement chamber, the top of broken case and the inside fixedly connected with dust exhausting fan that is located the dust removal case, there is the shrouding at the top of dust removal case through bolt swing joint, the equal fixedly connected with depression bar in both ends about the shrouding bottom, the bottom butt of depression bar has the slider, two fixedly connected with active carbon dust removal board between the relative one side of slider. This breaker is used in hydraulic engineering construction, when through to the material breakage, remove dust, both protected the surrounding environment, ensured staff's health simultaneously, and make things convenient for dismouting active carbon dust removal board, improved the life of active carbon dust removal board, be applicable to various circumstances.| (CN212549743)|HYDRAULIC ENGINEERING CONSTRUCTION(100,23)|BREAKER(100,11)|BROKEN GLASS CASE(100,11)|CRUSH BOX(100,10)|ENSURED STAFF HEALTH(78,1)|STAFF HEALTH(70,2)|BROKEN INCASEMENT CHAMBER(68,2)|BROKEN INCASEMENT CHAMBER SCREEN(48,1)|CRUSHING ROLLER(43,12)|CRUSHING BOX INNER CAVITY(43,4)|SCREEN CLOTH(42,2)|DUST(41,21)|PREVENTING DEPRESSION(37,3)|DEPRESSION BAR BOTTOM BUTT(36,1)|SLIDER(33,4)|NESTING(32,3)|SHROUDING BOTTOM(31,1)|LIFTING MOTOR(29,9)|CRUSHING BOX TOP(29,4)|POSITIVE TOP INTERCOMMUNICATION(28,4)|GROUND ROCK(28,3)|BOTTOM BUTT(26,1)|DEPRESSION(26,1)|EQUAL SWING(26,1)|MAKE THING(26,1)|SCREW CONVEYER(25,9)|CRUSHING BOX BOTTOM(21,4)|INNER CAVITY(20,11)|PRESSURE LEVER(20,7)|CLOTH(20,3)|HYDRAULIC ENGINEERING(19,2)|CRUSHING BOX LEFT BOTTOM(19,1)|EQUIPMENT BREAKAGE(19,1)|DISCHARGE HOLE(18,6)|FILTER SCREEN(18,5)|EQUAL DISAPPEARANCE(18,1)|DUST REMOVAL(17,35)|ACTIVE CARBON DUST REMOVAL(17,6)|SPOUT(17,4)|SLOPE(16,1)|ACTIVE CARBON DUST(15,2)|ACTIVE CARBON(14,6)|DUST TOP(13,3)|FIXING HOLE(13,3)|FAN(13,2)|INCLINE DIRECTION(13,1)|INNER CHAMBER BOTTOM(13,1)|ECCENTRIC WHEEL(12,8)|BOTTOM LEFT(12,1)|DUST REMOVAL CASE(11,6)|CONNECTING ROD(10,13)|SLIDING BLOCK(10,7)|INSIDE CAVITY(10,2)|SWING SIDE(10,1)|SEALING PLATE(9,13)|FEED PIPE(9,5)|INLET PIPE(9,3)|POSITIVE RIGHT(9,1)|GUIDE PLATE(8,13)|CRUSHING INNER CAVITY(8,4)|DRIVING MOTOR(7,9)|DIVIDE SIEVE(7,2)|NONEXCLUSIVE INCLUSION(7,1)|CONNECTING PIPE(6,12)|HOLE INCLINATION(6,4)|DISCHARGE VALVE(6,3)|SCREW AXIS(6,3)|SLIDING GROOVE(6,3)|SPIRAL SHAFT(6,3)|ELECTROMECHANICAL EQUIPMENT INSTALLER(6,1)|SCREEN CLOTH LEFT SIDE(6,1)|OUTPUT SHAFT(5,7)|SCREW SHAFT(5,3)|SERVICE LIFE(5,3)|POSITIVE RIGHT SIDE SWING(5,1)|SUCK DUST(5,1)|LEFT END(4,7)|UNQUALIFIED MATERIAL(4,4)|CRUSHING BOTTOM(4,2)|DUST REMOVAL FAN(4,2)|AMBIENT ENVIRONMENT(4,1)|BRACING PIECE(4,1)|DUST INNER CAVITY(4,1)|RELATIONAL TERM(4,1)|SPIRAL CONVEYER INNER CAVITY(4,1)|SWINGING MOTION(4,1)|SUPPORT ROD(3,5)|AIR FILTER(3,3)|CRUSHING(3,3)| (CN212549743)|1. The utility model provides a breaker for hydraulic engineering construction, includes broken case (1), its characterized in that: the dust removing device is characterized in that the left end and the right end of an inner cavity of the crushing box (1) are respectively and movably connected with a crushing roller (2), the top of the crushing box (1) is fixedly connected with a dust removing box (3), the bottom of the inner cavity of the crushing box (1) is fixedly connected with a filter screen (4), the top of the crushing box (1) is positioned in the dust removing box (3) and is fixedly connected with a dust removing fan (5), the top of the dust removing box (3) is movably connected with a sealing plate (6) through a bolt, the left end and the right end of the bottom of the sealing plate (6) are respectively and fixedly connected with a pressure lever (7), the bottom of the pressure lever (7) is abutted with a sliding block (8), two opposite sides of the sliding block (8) are respectively and fixedly connected with an active carbon dust removing plate (9), the left bottom of the crushing box (1, the positive right side swing joint of eccentric wheel (11) has connecting rod (12), the right side of connecting rod (12) articulates there is screen cloth (13), the left side of screen cloth (13) bottom articulates there is bracing piece (14), the right side fixedly connected with guide plate (15) of broken case (1) inner chamber bottom, the right side fixedly connected with screw conveyer (16) of broken case (1), the top fixedly connected with lifting motor (18) of screw conveyer (16), the output shaft fixedly connected with screw axis (17) of lifting motor (18), the positive top intercommunication of screw conveyer (16) has connecting pipe (19), the positive top intercommunication of broken case (1) has inlet pipe (20).|2. The crushing device for hydraulic engineering construction according to claim 1, wherein: the through-hole has been seted up at the top of shrouding (6), dust removal case (3) are inside cavity and the bottom and the cylindrical of the equal disappearance in top.|3. The crushing device for hydraulic engineering construction according to claim 1, wherein: the top at both ends all sets up the spout with slider (8) looks adaptation about dust removal case (3) inner chamber, and the top of spout and the top of dust removal case (3) are in the coplanar, depression bar (7) are located the inside of spout.|4. The crushing device for hydraulic engineering construction according to claim 1, wherein: the left side of the crushing box (1) is provided with a fixing hole, and the diameter of the fixing hole is larger than that of the connecting rod (12).|5. The crushing device for hydraulic engineering construction according to claim 1, wherein: the discharge hole is formed in the bottom of the crushing box (1), a discharge valve is fixedly connected to the bottom of the discharge hole, and support legs are fixedly connected to the periphery of the bottom of the crushing box (1).|6. The crushing device for hydraulic engineering construction according to claim 1, wherein: guide plate (15) and screen cloth (13) all are the slope form, and the incline direction is high right side low, guide plate (15) are located the right side of screen cloth (13) bottom. (CN212549743)|TECHNICAL FIELD|[0002] The utility model relates to a hydraulic engineering construction technical field specifically is a breaker for hydraulic engineering construction.|BACKGROUND ART|[0004] The hydraulic engineering construction has many same parts with the construction of general civil engineering such as roads, railways, bridges, house buildings and the like, for example, the main construction objects are mainly earthwork, stoneware, concrete, metal structures, electromechanical equipment installation and other projects, and some construction methods are the same.|[0005] Along with the development of science and technology, hydraulic engineering construction has become an independent subject, and the current breaker for hydraulic engineering construction in the market at present does not have the shortcoming of removing dust, and when using, breaker to the broken in-process of soil stone, can produce a large amount of dusts, and the dust is directly discharged into the air, has not only polluted the surrounding environment, has damaged staff's health simultaneously, so proposes above-mentioned breaker for hydraulic engineering construction in order to solve above-mentioned problem.|DISCLOSURE|[0006] SUMMERY OF THE UTILITY MODEL|[0007] Technical problem to be solved|[0008] Not enough to prior art, the utility model provides a breaker is used in hydraulic engineering construction possesses advantages such as dust removal, has solved when using, and breaker can produce a large amount of dusts to the broken in-process of soil stone, and the dust directly discharges into the air, has not only polluted the surrounding environment, has damaged staff's healthy problem simultaneously.|[0009] (II) technical scheme|[0010] In order to realize the above-mentioned purpose that possesses the dust removal, the utility model provides a following technical scheme: a crushing device for hydraulic engineering construction comprises a crushing box, wherein the left end and the right end of an inner cavity of the crushing box are movably connected with crushing rollers, the top of the crushing box is fixedly connected with a dust removal box, the bottom of the inner cavity of the crushing box is fixedly connected with a filter screen, the top of the crushing box is fixedly connected with a dust removal fan inside the dust removal box, the top of the dust removal box is movably connected with a sealing plate through a bolt, the left end and the right end of the bottom of the sealing plate are fixedly connected with pressure rods, the bottom of each pressure rod is abutted with a sliding block, an active carbon dust removal plate is fixedly connected between two opposite sides of the sliding blocks, the bottom of the left side of the crushing box is fixedly connected with a driving motor, an output shaft of the driving motor is fixedly connected with an eccentric wheel, the right side of the front side of the eccentric, the right side fixedly connected with guide plate of broken incasement chamber bottom, the right side fixedly connected with screw conveyer of broken case, screw conveyer's top fixedly connected with promotes the motor, promote the output shaft fixedly connected with screw axis of motor, the positive top intercommunication of screw conveyer has the connecting pipe, the positive top intercommunication of broken case has the inlet pipe.|[0011] Preferably, the through-hole has been seted up at the top of shrouding, the dust removal case is inside cavity and the bottom and the equal cylindrical of disappearance in top.|[0012] Preferably, the top at both ends all sets up the spout with slider looks adaptation about the dust removal case inner chamber, and the top of spout and the top of dust removal case are in the coplanar, the depression bar is located the inside of spout.|[0013] Preferably, a fixing hole is formed in the left side of the crushing box, and the diameter of the fixing hole is larger than that of the connecting rod.|[0014] Preferably, the bottom of the crushing box is provided with a discharge hole, the bottom of the discharge hole is fixedly connected with a discharge valve, and the periphery of the bottom of the crushing box is fixedly connected with support legs.|[0015] Preferably, the guide plate and the screen are both inclined, the inclination direction is high at the left and low at the right, and the guide plate is positioned on the right side of the bottom of the screen.|[0016] (III) advantageous effects|[0017] Compared with the prior art, the utility model provides a breaker is used in hydraulic engineering construction possesses following beneficial effect:|[0018] 1. the crushing device for hydraulic engineering construction controls the dust removal fan to work by the external controller in the crushing process, the dust removal fan sucks dust into the dust removal box, large-particle fragments in the dust are filtered by the filter screen, fine particles in the dust are adsorbed and filtered by the activated carbon dust removal plate, and the filtered air is discharged through the through hole in the top of the sealing plate, so that dust removal is realized, the sealing plate is dismounted, the top of the chute and the top of the dust removal box are in the same plane, so that the activated carbon dust removal plate is convenient to take off and maintain, the arrangement of the pressure rod is convenient to fix the activated carbon dust removal plate, the device removes dust when materials are crushed, the ambient environment is protected, the health of workers is guaranteed, the activated carbon dust removal plate is convenient to dismount and mount, and the service life of the activated carbon dust removal plate is prolonged, is suitable for various conditions.|[0019] 2. The crushing device for hydraulic engineering construction comprises a feeding pipe, a crushing box, a driving motor, an eccentric wheel, a connecting rod, a crushing roller, a screen, a guide plate, a screw conveyor, a lifting motor, a screw shaft, a connecting pipe, a connecting rod, a crushing roller, a baffle plate, a connecting rod, a supporting rod, a lifting motor, a screw shaft, a lifting motor, a connecting pipe, a feeding pipe, a connecting pipe, a baffle plate, a connecting pipe, a connecting, is convenient to use.|DRAWINGS DESCRIPTION|[0021] FIG. 1 is a schematic structural view of the present invention;|[0022] FIG. 2 is an enlarged view of the point A in FIG. 1 according to the present invention;|[0023] FIG. 3 is an external view of the present invention;|[0024] fig. 4 is a top view of the crushing box and the screw conveyer of the present invention.|[0025] In the figure: 1 crushing box, 2 crushing rollers, 3 dust removing box, 4 filter screen, 5 dust removing fan, 6 sealing plate, 7 pressure bar, 8 slide block, 9 active carbon dust removing plate, 10 driving motor, 11 eccentric wheel, 12 connecting rod, 13 screen, 14 supporting rod, 15 guide plate, 16 screw conveyer, 17 screw shaft, 18 lifting motor, 19 connecting pipe, 20 feeding pipe.|INVENTION MODE|[0026] Detailed Description|[0027] The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.|[0028] Referring to fig. 1-4, a crushing device for hydraulic engineering construction comprises a crushing box 1, wherein a discharge hole is formed in the bottom of the crushing box 1, a discharge valve is fixedly connected to the bottom of the discharge hole, support legs are fixedly connected to the periphery of the bottom of the crushing box 1, crushing rollers 2 are movably connected to the left end and the right end of an inner cavity of the crushing box 1, the crushing rollers 2 are in transmission connection with an external motor, a dust removal box 3 is fixedly connected to the top of the crushing box 1, a filter screen 4 is fixedly connected to the bottom of the inner cavity of the crushing box 1, a dust removal fan 5 is fixedly connected to the top of the crushing box 1 and inside the dust removal box 3, the type of the dust removal fan 5 can be DFA150, the filter screen 4 is located at the bottom of an air inlet of the dust removal fan 5, a sealing plate 6 is movably connected to the top of the dust removal box 3 through bolts, a through hole, the left end and the right end of the bottom of the sealing plate 6 are fixedly connected with a pressure lever 7, the bottom of the pressure lever 7 penetrates through and extends into the side wall of the dust removing box 3 and is connected with the dust removing box 3 in a sliding manner, the bottom of the pressure lever 7 is abutted with a sliding block 8, sliding grooves matched with the sliding block 8 are formed in the top of the left end and the right end of the inner cavity of the dust removing box 3, the top of each sliding groove and the top of the dust removing box 3 are positioned in the same plane, the pressure lever 7 is positioned in the sliding grooves, an activated carbon dust removing plate 9 is fixedly connected between the opposite sides of the two sliding blocks 8, the bottom of the left side of the crushing box 1 is fixedly connected with a driving motor 10, the model of the driving motor 10 can be A155S45F, an output shaft of the driving motor 10 is fixedly connected with an eccentric wheel 11, the right side of the front of the eccentric wheel 11 is, the inclined plate is positioned above the connecting rod 12 and below the left crushing roller 2, the right side of the connecting rod 12 penetrates through and extends into the crushing box 1, the right side of the connecting rod 12 is hinged with a screen 13, the left side of the bottom of the screen 13 is hinged with a support rod 14, the bottom of the support rod 14 is fixedly connected with the left side of the bottom of the inner cavity of the crushing box 1, the right side of the bottom of the inner cavity of the crushing box 1 is fixedly connected with a guide plate 15, the guide plate 15 and the screen 13 are both inclined and the inclination direction is high at the left and low at the right, the guide plate 15 is positioned on the right side of the bottom of the screen 13, the right side of the crushing box 1 is fixedly connected with a spiral conveyor 16, the bottom of the right side of the spiral conveyor 16 is provided with an inclined hole, the inclined hole is communicated with the bottom of the left side of the spiral conveyor 16, the type of the lifting motor 18 can be ECMA-C20604RS, an output shaft of the lifting motor 18 is fixedly connected with a spiral shaft 17, the bottom of the spiral shaft 17 is movably connected with the bottom of an inner cavity of the spiral conveyor 16, the top of the front surface of the spiral conveyor 16 is communicated with a connecting pipe 19, the connecting pipe 19 is inclined, the inclined angle is high at the right side and low at the left side, the top of the front surface of the crushing box 1 is communicated with a feeding pipe 20, the feeding pipe 20 is inclined, the inclined direction is that one end close to the crushing box 1 is low and the other end far away from the crushing box 1 is high, the position of the feeding pipe 20 corresponds to a gap between two opposite sides of the crushing rollers 2, the right side of the feeding pipe 20 is communicated with the left side of the connecting pipe 19, in the crushing process, the work of the dust removal fan 5 is controlled by an external controller, the dust removal fan 5 sucks dust, meanwhile, fine particles in dust are adsorbed and filtered through the activated carbon dust removal plate 9, filtered air is discharged through a through hole in the top of the sealing plate 6, dust removal is realized, the sealing plate 6 is disassembled, the top of the chute and the top of the dust removal box 3 are in the same plane, the activated carbon dust removal plate 9 is convenient to take down and maintain, the pressure rod 7 is arranged to fix the activated carbon dust removal plate 9 conveniently, when the device is used for crushing materials, dust removal is performed, the surrounding environment is protected, the health of workers is guaranteed, the activated carbon dust removal plate 9 is convenient to disassemble and assemble, the service life of the activated carbon dust removal plate 9 is prolonged, the device is suitable for various conditions, the materials enter the crushing box 1 through the material inlet pipe 20, the external motor drives the crushing roller 2 to rotate and crush the materials, the crushed materials enter the screen 13, driving motor 10 works, driving motor 10 drives eccentric wheel 11 rotatory, and it is the swing motion along bracing piece 14 to drive screen cloth 13 through connecting rod 12, thereby screen out the material, the material that qualifies then enters into the bottom of broken case 1 inner chamber, and unqualified material then enters into screw conveyer 16 inside through guide plate 15 and inclined hole, the output shaft that promotes motor 18 drives screw axis 17 work, and promote the material, and enter into broken case 1 inside again through connecting pipe 19 and inlet pipe 20, crushing roller 2 carries out the secondary crushing to unqualified material, the device is through carrying out the breakage to the material, divide sieve and secondary crushing, thereby reach the purpose that crushing effect is good, efficiency and quality when having accelerated the breakage, and convenient to use.|[0029] To sum up, the crushing device for hydraulic engineering construction controls the operation of the dust removing fan 5 by the external controller in the crushing process, the dust removing fan 5 sucks dust into the dust removing box 3, large-particle fragments in the dust are filtered by the filter screen 4, fine particles in the dust are adsorbed and filtered by the activated carbon dust removing plate 9, the filtered air is discharged through the through hole at the top of the sealing plate 6, so that dust removal is realized, meanwhile, the sealing plate 6 is dismounted, because the top of the chute and the top of the dust removing box 3 are in the same plane, the activated carbon dust removing plate 9 is convenient to take down and maintain, the activated carbon dust removing plate 9 is convenient to fix by the arrangement of the pressure lever 7, when the device crushes materials, dust removal is performed, the surrounding environment is protected, the health of workers is ensured at the same time, and the activated carbon dust removing plate 9 is convenient to dismount, the service life of the active carbon dust removal plate 9 is prolonged, the active carbon dust removal plate is suitable for various conditions, materials enter a crushing box 1 from a feeding pipe 20 through materials, an external motor drives a crushing roller 2 to rotate and crush the materials, the crushed materials enter a screen 13, a driving motor 10 works, the driving motor 10 drives an eccentric wheel 11 to rotate and drives the screen 13 to swing along a support rod 14 through a connecting rod 12, so that the materials are screened out, qualified materials enter the bottom of an inner cavity of the crushing box 1, unqualified materials enter a spiral conveyor 16 through a guide plate 15 and an inclined hole, an output shaft of a lifting motor 18 drives a spiral shaft 17 to work and lift the materials, the materials enter the crushing box 1 again through a connecting pipe 19 and the feeding pipe 20, the crushing roller 2 performs secondary crushing on unqualified materials, and the device performs secondary crushing on the materials through crushing, Divide sieve and secondary crushing to reach the purpose that the crushing effect is good, efficiency and quality when having accelerated the breakage, facilitate the use, solved when using, breaker can produce a large amount of dusts to the broken in-process of soil stone, and the dust directly discharges into the air, has not only polluted the surrounding environment, has damaged the healthy problem of staff simultaneously.|[0030] It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.|[0031] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. (CN212549743)|TECHNICAL FIELD|[0002] The utility model relates to a hydraulic engineering construction technical field specifically is a breaker for hydraulic engineering construction.|BACKGROUND ART|[0004] The hydraulic engineering construction has many same parts with the construction of general civil engineering such as roads, railways, bridges, house buildings and the like, for example, the main construction objects are mainly earthwork, stoneware, concrete, metal structures, electromechanical equipment installation and other projects, and some construction methods are the same.|[0005] Along with the development of science and technology, hydraulic engineering construction has become an independent subject, and the current breaker for hydraulic engineering construction in the market at present does not have the shortcoming of removing dust, and when using, breaker to the broken in-process of soil stone, can produce a large amount of dusts, and the dust is directly discharged into the air, has not only polluted the surrounding environment, has damaged staff's health simultaneously, so proposes above-mentioned breaker for hydraulic engineering construction in order to solve above-mentioned problem.|DISCLOSURE|[0006] SUMMERY OF THE UTILITY MODEL|[0007] Technical problem to be solved|[0008] Not enough to prior art, the utility model provides a breaker is used in hydraulic engineering construction possesses advantages such as dust removal, has solved when using, and breaker can produce a large amount of dusts to the broken in-process of soil stone, and the dust directly discharges into the air, has not only polluted the surrounding environment, has damaged staff's healthy problem simultaneously.|[0009] (II) technical scheme|[0010] In order to realize the above-mentioned purpose that possesses the dust removal, the utility model provides a following technical scheme: a crushing device for hydraulic engineering construction comprises a crushing box, wherein the left end and the right end of an inner cavity of the crushing box are movably connected with crushing rollers, the top of the crushing box is fixedly connected with a dust removal box, the bottom of the inner cavity of the crushing box is fixedly connected with a filter screen, the top of the crushing box is fixedly connected with a dust removal fan inside the dust removal box, the top of the dust removal box is movably connected with a sealing plate through a bolt, the left end and the right end of the bottom of the sealing plate are fixedly connected with pressure rods, the bottom of each pressure rod is abutted with a sliding block, an active carbon dust removal plate is fixedly connected between two opposite sides of the sliding blocks, the bottom of the left side of the crushing box is fixedly connected with a driving motor, an output shaft of the driving motor is fixedly connected with an eccentric wheel, the right side of the front side of the eccentric, the right side fixedly connected with guide plate of broken incasement chamber bottom, the right side fixedly connected with screw conveyer of broken case, screw conveyer's top fixedly connected with promotes the motor, promote the output shaft fixedly connected with screw axis of motor, the positive top intercommunication of screw conveyer has the connecting pipe, the positive top intercommunication of broken case has the inlet pipe.|[0011] Preferably, the through-hole has been seted up at the top of shrouding, the dust removal case is inside cavity and the bottom and the equal cylindrical of disappearance in top.|[0012] Preferably, the top at both ends all sets up the spout with slider looks adaptation about the dust removal case inner chamber, and the top of spout and the top of dust removal case are in the coplanar, the depression bar is located the inside of spout.|[0013] Preferably, a fixing hole is formed in the left side of the crushing box, and the diameter of the fixing hole is larger than that of the connecting rod.|[0014] Preferably, the bottom of the crushing box is provided with a discharge hole, the bottom of the discharge hole is fixedly connected with a discharge valve, and the periphery of the bottom of the crushing box is fixedly connected with support legs.|[0015] Preferably, the guide plate and the screen are both inclined, the inclination direction is high at the left and low at the right, and the guide plate is positioned on the right side of the bottom of the screen.|[0016] (III) advantageous effects|[0017] Compared with the prior art, the utility model provides a breaker is used in hydraulic engineering construction possesses following beneficial effect:|[0018] 1. the crushing device for hydraulic engineering construction controls the dust removal fan to work by the external controller in the crushing process, the dust removal fan sucks dust into the dust removal box, large-particle fragments in the dust are filtered by the filter screen, fine particles in the dust are adsorbed and filtered by the activated carbon dust removal plate, and the filtered air is discharged through the through hole in the top of the sealing plate, so that dust removal is realized, the sealing plate is dismounted, the top of the chute and the top of the dust removal box are in the same plane, so that the activated carbon dust removal plate is convenient to take off and maintain, the arrangement of the pressure rod is convenient to fix the activated carbon dust removal plate, the device removes dust when materials are crushed, the ambient environment is protected, the health of workers is guaranteed, the activated carbon dust removal plate is convenient to dismount and mount, and the service life of the activated carbon dust removal plate is prolonged, is suitable for various conditions.|[0019] 2. The crushing device for hydraulic engineering construction comprises a feeding pipe, a crushing box, a driving motor, an eccentric wheel, a connecting rod, a crushing roller, a screen, a guide plate, a screw conveyor, a lifting motor, a screw shaft, a connecting pipe, a connecting rod, a crushing roller, a baffle plate, a connecting rod, a supporting rod, a lifting motor, a screw shaft, a lifting motor, a connecting pipe, a feeding pipe, a connecting pipe, a baffle plate, a connecting pipe, a connecting, is convenient to use.|DRAWINGS DESCRIPTION|[0021] FIG. 1 is a schematic structural view of the present invention;|[0022] FIG. 2 is an enlarged view of the point A in FIG. 1 according to the present invention;|[0023] FIG. 3 is an external view of the present invention;|[0024] fig. 4 is a top view of the crushing box and the screw conveyer of the present invention.|[0025] In the figure: 1 crushing box, 2 crushing rollers, 3 dust removing box, 4 filter screen, 5 dust removing fan, 6 sealing plate, 7 pressure bar, 8 slide block, 9 active carbon dust removing plate, 10 driving motor, 11 eccentric wheel, 12 connecting rod, 13 screen, 14 supporting rod, 15 guide plate, 16 screw conveyer, 17 screw shaft, 18 lifting motor, 19 connecting pipe, 20 feeding pipe.|INVENTION MODE|[0026] Detailed Description|[0027] The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.|[0028] Referring to fig. 1-4, a crushing device for hydraulic engineering construction comprises a crushing box 1, wherein a discharge hole is formed in the bottom of the crushing box 1, a discharge valve is fixedly connected to the bottom of the discharge hole, support legs are fixedly connected to the periphery of the bottom of the crushing box 1, crushing rollers 2 are movably connected to the left end and the right end of an inner cavity of the crushing box 1, the crushing rollers 2 are in transmission connection with an external motor, a dust removal box 3 is fixedly connected to the top of the crushing box 1, a filter screen 4 is fixedly connected to the bottom of the inner cavity of the crushing box 1, a dust removal fan 5 is fixedly connected to the top of the crushing box 1 and inside the dust removal box 3, the type of the dust removal fan 5 can be DFA150, the filter screen 4 is located at the bottom of an air inlet of the dust removal fan 5, a sealing plate 6 is movably connected to the top of the dust removal box 3 through bolts, a through hole, the left end and the right end of the bottom of the sealing plate 6 are fixedly connected with a pressure lever 7, the bottom of the pressure lever 7 penetrates through and extends into the side wall of the dust removing box 3 and is connected with the dust removing box 3 in a sliding manner, the bottom of the pressure lever 7 is abutted with a sliding block 8, sliding grooves matched with the sliding block 8 are formed in the top of the left end and the right end of the inner cavity of the dust removing box 3, the top of each sliding groove and the top of the dust removing box 3 are positioned in the same plane, the pressure lever 7 is positioned in the sliding grooves, an activated carbon dust removing plate 9 is fixedly connected between the opposite sides of the two sliding blocks 8, the bottom of the left side of the crushing box 1 is fixedly connected with a driving motor 10, the model of the driving motor 10 can be A155S45F, an output shaft of the driving motor 10 is fixedly connected with an eccentric wheel 11, the right side of the front of the eccentric wheel 11 is, the inclined plate is positioned above the connecting rod 12 and below the left crushing roller 2, the right side of the connecting rod 12 penetrates through and extends into the crushing box 1, the right side of the connecting rod 12 is hinged with a screen 13, the left side of the bottom of the screen 13 is hinged with a support rod 14, the bottom of the support rod 14 is fixedly connected with the left side of the bottom of the inner cavity of the crushing box 1, the right side of the bottom of the inner cavity of the crushing box 1 is fixedly connected with a guide plate 15, the guide plate 15 and the screen 13 are both inclined and the inclination direction is high at the left and low at the right, the guide plate 15 is positioned on the right side of the bottom of the screen 13, the right side of the crushing box 1 is fixedly connected with a spiral conveyor 16, the bottom of the right side of the spiral conveyor 16 is provided with an inclined hole, the inclined hole is communicated with the bottom of the left side of the spiral conveyor 16, the type of the lifting motor 18 can be ECMA-C20604RS, an output shaft of the lifting motor 18 is fixedly connected with a spiral shaft 17, the bottom of the spiral shaft 17 is movably connected with the bottom of an inner cavity of the spiral conveyor 16, the top of the front surface of the spiral conveyor 16 is communicated with a connecting pipe 19, the connecting pipe 19 is inclined, the inclined angle is high at the right side and low at the left side, the top of the front surface of the crushing box 1 is communicated with a feeding pipe 20, the feeding pipe 20 is inclined, the inclined direction is that one end close to the crushing box 1 is low and the other end far away from the crushing box 1 is high, the position of the feeding pipe 20 corresponds to a gap between two opposite sides of the crushing rollers 2, the right side of the feeding pipe 20 is communicated with the left side of the connecting pipe 19, in the crushing process, the work of the dust removal fan 5 is controlled by an external controller, the dust removal fan 5 sucks dust, meanwhile, fine particles in dust are adsorbed and filtered through the activated carbon dust removal plate 9, filtered air is discharged through a through hole in the top of the sealing plate 6, dust removal is realized, the sealing plate 6 is disassembled, the top of the chute and the top of the dust removal box 3 are in the same plane, the activated carbon dust removal plate 9 is convenient to take down and maintain, the pressure rod 7 is arranged to fix the activated carbon dust removal plate 9 conveniently, when the device is used for crushing materials, dust removal is performed, the surrounding environment is protected, the health of workers is guaranteed, the activated carbon dust removal plate 9 is convenient to disassemble and assemble, the service life of the activated carbon dust removal plate 9 is prolonged, the device is suitable for various conditions, the materials enter the crushing box 1 through the material inlet pipe 20, the external motor drives the crushing roller 2 to rotate and crush the materials, the crushed materials enter the screen 13, driving motor 10 works, driving motor 10 drives eccentric wheel 11 rotatory, and it is the swing motion along bracing piece 14 to drive screen cloth 13 through connecting rod 12, thereby screen out the material, the material that qualifies then enters into the bottom of broken case 1 inner chamber, and unqualified material then enters into screw conveyer 16 inside through guide plate 15 and inclined hole, the output shaft that promotes motor 18 drives screw axis 17 work, and promote the material, and enter into broken case 1 inside again through connecting pipe 19 and inlet pipe 20, crushing roller 2 carries out the secondary crushing to unqualified material, the device is through carrying out the breakage to the material, divide sieve and secondary crushing, thereby reach the purpose that crushing effect is good, efficiency and quality when having accelerated the breakage, and convenient to use.|[0029] To sum up, the crushing device for hydraulic engineering construction controls the operation of the dust removing fan 5 by the external controller in the crushing process, the dust removing fan 5 sucks dust into the dust removing box 3, large-particle fragments in the dust are filtered by the filter screen 4, fine particles in the dust are adsorbed and filtered by the activated carbon dust removing plate 9, the filtered air is discharged through the through hole at the top of the sealing plate 6, so that dust removal is realized, meanwhile, the sealing plate 6 is dismounted, because the top of the chute and the top of the dust removing box 3 are in the same plane, the activated carbon dust removing plate 9 is convenient to take down and maintain, the activated carbon dust removing plate 9 is convenient to fix by the arrangement of the pressure lever 7, when the device crushes materials, dust removal is performed, the surrounding environment is protected, the health of workers is ensured at the same time, and the activated carbon dust removing plate 9 is convenient to dismount, the service life of the active carbon dust removal plate 9 is prolonged, the active carbon dust removal plate is suitable for various conditions, materials enter a crushing box 1 from a feeding pipe 20 through materials, an external motor drives a crushing roller 2 to rotate and crush the materials, the crushed materials enter a screen 13, a driving motor 10 works, the driving motor 10 drives an eccentric wheel 11 to rotate and drives the screen 13 to swing along a support rod 14 through a connecting rod 12, so that the materials are screened out, qualified materials enter the bottom of an inner cavity of the crushing box 1, unqualified materials enter a spiral conveyor 16 through a guide plate 15 and an inclined hole, an output shaft of a lifting motor 18 drives a spiral shaft 17 to work and lift the materials, the materials enter the crushing box 1 again through a connecting pipe 19 and the feeding pipe 20, the crushing roller 2 performs secondary crushing on unqualified materials, and the device performs secondary crushing on the materials through crushing, Divide sieve and secondary crushing to reach the purpose that the crushing effect is good, efficiency and quality when having accelerated the breakage, facilitate the use, solved when using, breaker can produce a large amount of dusts to the broken in-process of soil stone, and the dust directly discharges into the air, has not only polluted the surrounding environment, has damaged the healthy problem of staff simultaneously.|[0030] It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.|[0031] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. Family Number|(92807669)|92807669|Abstract|(CN212549743U U)|The utility model relates to the technical field of water conservancy project construction , and discloses a crushing device for water conservancy project construction , which comprises a crushing box , crushing rollers are movably connected to the left end and the right end of an inner cavity of the crushing box , a dust removal box is fixedly connected to the top of the crushing box , and a filter screen is fixedly connected to the bottom of the inner cavity of the crushing box . A dust removal fan is fixedly connected to the position , located in the dust removal box , of the top of the crushing box , a sealing plate is movably connected to the top of the dust removal box through bolts , pressing rods are fixedly connected to the left end and the right end of the bottom of the sealing plate , andthe bottoms of the pressing rods abut against sliding blocks ; an activated carbon dust removal plate is fixedly connected between the opposite sides of the two sliding blocks . According to the crushing device for hydraulic engineering construction , when materials are crushed , dust is removed , the surrounding environment is protected , meanwhile , the health of workers is guaranteed , the activated carbon dust removal plate is convenient to disassemble and assemble , the service life of the activated carbon dust removal plate is prolonged , and the crushing device is suitable for various conditions . |IPC codes|(CN212549743U U)|B01D - 046/12 |Title|(CN212549743U U)|Crushing device for hydraulic engineering construction | Chemical engineering|Environmental technology B01D-046/12|B02C-004/08|B02C-004/28|B02C-023/12|B02C-023/24|B07B-001/28|B07B-001/42|B07B-001/46 B01D-046/12|B02C-004/08|B02C-004/28|B02C-023/12|B02C-023/24|B07B-001/28|B07B-001/42|B07B-001/46 CN114832933|CN114289299B CN114832933 101160490 WHO=Examiner SELF=N CAT=A|CN114289299B 99519254 WHO=Examiner SELF=N LAPSED (CN212549743)|LAPSED DEAD (CN212549743)|DEAD (CN212549743)|LEGAL DETAILS FOR CN212549743|Actual or expected expiration date=2023-05-23|Legal state=DEAD|Status=LAPSED|Event publication date=2020-05-19|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202020841099|Application date=2020-05-19|Standardized application number=2020CN-U841099|Event publication date=2021-02-19|Event code=CN/U|Event indicator=Pos|Event group=Event indicating In Force|Registered Utility Model|Publication country=CN|Publication number=CN212549743|Publication stage code=U|Publication date=2021-02-19|Standardized publication number=CN212549743U|Event publication date=2021-02-19|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2023-05-23|Event code=CN/CF01|Event indicator=Neg|Event group=Event indicating Not In Force|Termination of patent right due to non-payment of annual fee https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=jf59U3ybGzasahl6qo38yqqLeopS8oZMbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000055934619&ekey=1916&xpn=CN212549743U&kind=U https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=QQvh0Z5ugGg358jssuer37msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN212549743)|CN (CN212549743)|NAME=LUO SHAOFENG , COUNTRY=CN (CN212549743)|NAME=CAO YUQING;BEIJING JINCHUANG INTELLECTUAL PROPERTY AGENCY FIRM , REG=11589 (CN212549743)|NAME=LUO SHAOFENG 0 1 Titre: (CN212549743)|Crushing device for hydraulic engineering construction Résumé: (CN212549743)|The utility model relates to the technical field of water conservancy project construction, and discloses a crushing device for water conservancy project construction, which comprises a crushing box,crushing rollers are movably connected to the left end and the right end of an inner cavity of the crushing box, a dust removal box is fixedly connected to the top of the crushing box, and a filter screen is fixedly connected to the bottom of the inner cavity of the crushing box. A dust removal fan is fixedly connected to the position, located in the dust removal box, of the top of the crushing box, a sealing plate is movably connected to the top of the dust removal box through bolts, pressing rods are fixedly connected to the left end and the right end of the bottom of the sealing plate, andthe bottoms of the pressing rods abut against sliding blocks; an activated carbon dust removal plate is fixedly connected between the opposite sides of the two sliding blocks. According to the crushing device for hydraulic engineering construction, when materials are crushed, dust is removed, the surrounding environment is protected, meanwhile, the health of workers is guaranteed, the activated carbon dust removal plate is convenient to disassemble and assemble, the service life of the activated carbon dust removal plate is prolonged, and the crushing device is suitable for various conditions. 59 Abstract gpt-4o-mini no The article describes a crushing device for hydraulic engineering construction, focusing on dust removal and worker safety, with no mention of enhanced weathering or CO₂ capture.
60 CN202511707827 CN202511707827 CN121454002 117662153 CN121454002 A 2026-02-03 [CN121454002] 2025-11-20 2025-11-20 2026-02-03 (CN121454002)|2045-11-20 (CN121454002)|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions (CN121454002)|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of rock weathering and carbon sequestration enhancement, mineral fertilizer development and saline soil improvement and treatment. The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions. The leaching equipment comprises a temperature control device, a leaching assembly, a rainfall simulation device, a temperature and humidity sensor and a controller, wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame. The leaching assembly comprises a leaching column arranged in the constant-temperature box device and a liquid collecting container arranged below the leaching column. The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline-alkali soil; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners, novel mineral fertilizers and saline-alkali soil improvement. LANZHOU UNIVERSITY|MICROCARBON LOW CARBON TECHNOLOGY (CN121454002)|LANZHOU UNIVERSITY ([CN])|Microcarbon (Guangzhou) Low Carbon Technology Co., Ltd. ZHANG JIETANG|LI XINGYUAN|GOU XIAOHUA (CN121454002)|ZHANG JIETANG|LI XINGYUAN|GOU XIAOHUA (CN121454002)|HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 41028 (CN121454002)|It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves.|The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain.|Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.|In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device: (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition;| (CN121454002)|1. An leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, comprising: The temperature control device comprises a support frame and an incubator device arranged on the support frame; The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.| (CN121454002)|In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of enhanced rock weathering carbon fixation, mineral fertilizer development and saline soil improvement and management.| (CN121454002)|LEACHING COLUMN(100,88)|POWDER(100,60)|SILICATE(100,50)|NATURAL TEMPERATURE(100,30)|SIMULATING CHEMICAL WEATHERING(100,27)|HUMIDITY CONDITION(100,16)|LEACHING EQUIPMENT(100,7)|SYNCHRONOUS PULLEY(77,6)|RAINFALL SIMULATION(74,20)|LINK ROD(71,15)|LEACHING(65,36)|INCUBATOR(54,39)|CHEMICAL WEATHERING LEACHING EXPERIMENT(51,2)|MULTIFUNCTIONAL SILICATE MINERAL DEVELOPMENT(49,3)|LABORATORY SIMULATION SILICATE MINERAL(48,1)|LEACHING EXPERIMENT(47,3)|MULTIFUNCTIONAL SILICATE MINERAL(46,3)|NUTRIENT RELEASE(44,2)|HUMIDITY(41,34)|RELIABLE SILICATE MINERAL(41,2)|INJECTION CYLINDER(40,23)|SIMULATED RAINFALL(39,5)|COLUMNAR ROCK MASS(39,3)|MINERAL FERTILIZER DEVELOPMENT(39,1)|ENHANCED ROCK(38,1)|LIQUID COLLECTION CONTAINER(35,10)|SILICATE HUMIDITY(35,3)|NATURAL RAINFALL(34,6)|LINKAGE ROD(33,26)|SALINE ALKALI SOIL(33,17)|SALINE SOIL IMPROVEMENT(33,1)|SEAT SUPPORT(32,17)|SILICATE MINERAL(31,19)|CIRCULATION AIR DUCT(31,5)|CHEMICAL WEATHERING(28,18)|NATURAL CONDITION(28,2)|AIR CIRCULATION(24,15)|CONTROLLABLE TEMPERATURE(24,3)|HUMIDITY SENSOR(23,18)|LEACHING SOLUTION(22,20)|REFRIGERATOR(22,10)|DRIVING PISTON(22,6)|PUSH PULL ROD(21,17)|MINERAL FERTILIZER(21,5)|EXPERIMENTAL SUPPORT(20,4)|LEACHING SOLUTION PUMPING(20,2)|DEVIATION(20,1)|THERMOSTAT(20,1)|SILICATE TEMPERATURE(19,3)|HUMIDITY ENVIRONMENT(19,2)|LEACHING CHAMBER(19,2)|SLIDING HOLE(18,6)|SOIL TEMPERATURE(18,4)|NATURAL PRECIPITATION CONDITION(18,2)|LABORATORY(18,1)|INFUSION TUBE(17,2)|SILICATE MINERAL CHEMICAL WEATHERING(16,7)|CONDITIONING AGENT(16,3)|SPRAY BRACKET(16,3)|HEAT PIPE(16,2)|MESH PLATE(15,7)|SILICATE RELATIVE HUMIDITY(14,3)|LIQUID DELIVERY PIPE(14,2)|SUPPORTING SPRAY(14,2)|SYRINGE PUMP DRIVING(14,2)|SOLENOID VALVE(14,1)|LIQUID INLET(13,10)|LIQUID OUTLET(13,10)|LARGE DEVIATION(13,1)|LIQUID ADDITION(13,1)|SUPPORT FRAME(12,14)|CIRCULATION DUCT(12,5)|TEMPERATURE DETECTION(12,5)|FILTER SCREEN(12,4)|SYRINGE PUMP SUPPORT(12,3)|LINK LEVER(11,9)|CARBON FIXATION(11,4)|NATURAL ENVIRONMENT(11,4)|EQUAL LENGTH LINK ROD(11,3)|DRIVING SHAFT(10,24)|INJECTION PUMP(10,19)|DRIVING LEVER(10,7)|DRIVING MOTOR SHAFT(10,2)|RAINFALL SIMULATOR(10,2)|SUPPORT BASE(10,2)|LEACHING COLUMN END(9,5)|PRESET TEMPERATURE(9,5)|SILICATE ROCK POWDER(9,2)|EXPERIMENTAL SIMULATION AUTHENTICITY(9,1)|LIQUID STORAGE CONTAINER(8,7)|CHEMICAL WEATHERING SIMULATION EXPERIMENT(8,3)|TIMING PULLEY(8,3)|OPEN SHAPE(8,2)|MULTIFUNCTIONAL SILICATE MINERAL CONDITIONER(8,1)|DRIVING ROD(7,7)|RELATIVE HUMIDITY(7,3)|AIR RETURN OPENING(7,1)|NUTRIENT SUPPLEMENTATION(7,1)|REAL RAINFALL SIMULATION(7,1)|SILICATE POWDER DISTURBANCE(7,1)|GEAR(6,11)|CARBON FIXING PROCESS DATA(6,3)|SHOWER SOLUTION(6,3)|SYNCHRONOUS BELT WHEEL(6,3)|WATER INLET PIPE(6,3)|DETECTING LEACHING LIQUID PRESSURE(6,2)|HEATING AIR(6,2)|NATURAL SALINE ALKALI SOIL(6,2)|PRECIPITATION MINERAL CHEMICAL WEATHERING(6,2)|RAINFALL SIMULATION DIAGRAM(6,2)|RELIABLE WEATHERING REACTION(6,2)|CONSTANT TEMPERATURE CAVITY INSIDE(6,1)|LEACHING EXPERIMENT ACCURACY(6,1)|RESEARCH SCIENTIFICITY(6,1)|SALINE SOIL RECONSTRUCTION TREATMENT(6,1)|SILICATE DISTURBANCE(6,1)|SIMULATING LEACHING(6,1)|PRESSURE SENSOR(5,7)|AIR RETURN PIPE(5,4)|INNER HOLE WALL(5,4)|COLUMN ROCK MASS(5,2)|TEMPERATURE REGULATION(5,2)|TRANSFUSION TUBE(5,2)|EXPERIMENTAL VERIFICATION(5,1)|NOZZLE ATOMIZATION(5,1)|OUTER CIRCUMFERENTIAL SURFACE(5,1)|PAYING ATTENTION(5,1)|PRECIPITATION SIMULATION(5,1)|SALINE ALKALI SOIL HUMIDITY(5,1)|SILICATE POWDER LEACHING SOLUTION(5,1)|SUCKING LEACHING SOLUTION(5,1)|TRANSPARENT OBSERVATION WINDOW(5,1)|CONNECTING ROD(4,20)|HEATING COMPONENT(4,5)|CHEMICAL WEATHERING EXPERIMENT(4,2)|HUMIDITY SENSOR FEED(4,2)|INCUBATOR CONSTANT TEMPERATURE CAVITY(4,2)|SPRAY COMPONENT(4,2)|SPRAYING SUPPORT(4,2)|SYRINGE DIRECTION(4,2)|TRUE ACCURACY(4,2)|1244 CIRCULATION FAN(4,1)|ATOMIZING SPRAY HEAD(4,1)|INCUBATOR HEATING(4,1)|INSUFFICIENT NUTRIENT SUPPLY(4,1)|LEACHING CAVITY(4,1)|LEACHING SOLUTION CONCENTRATED IMPACT(4,1)|LEACHING SOLUTION UNIFORMITY(4,1)|PRESET HUMIDITY(4,1)|CHAMBER DOOR(3,1)|COLUMNAR ROCK TOP(3,1)|CONSTANT TEMPERATURE INTRACAVITY REFRIGERATOR(3,1)|HEAT PRESERVATION BOX(3,1)|LEACHING COLUMN OPENING(3,1)|MINERAL CONDITIONING AGENT DEVELOPMENT(3,1)|MODIFIER(3,1)|REAL SOIL CHANGE(3,1)| (CN121454002)|1. An leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, comprising:| The temperature control device comprises a support frame and an incubator device arranged on the support frame; | The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; | a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; | a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and |And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.|2. The leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions according to claim 1, wherein the rainfall simulation device comprises a spraying assembly arranged at an opening at the top end of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying assembly and a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the controller can control the driving device, the first valve and the second valve to work, and the driving device and the second valve are respectively electrically connected with the controller.|3. The leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 2, wherein the injection pump mechanism comprises an injection cylinder with two open ends, a first piston arranged in the injection cylinder in a sliding manner, a second piston arranged in the injection cylinder in a sliding manner, a push-pull rod for driving the first piston to move along the axial direction of the injection cylinder, a first linkage rod connected with one end of the push-pull rod far away from the first piston, a sleeve for driving the second piston to move along the axial direction of the injection cylinder, and a second linkage rod connected with one end of the sleeve far away from the second piston, wherein a first sliding hole for the push-pull rod to pass through is arranged on the second piston, the outer circumferential surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve is sleeved on the rod in an axial sliding manner, and the first linkage rod and the second linkage rod are respectively connected with the driving device.|4. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 3, wherein the driving means comprises a driving assembly, a link mechanism connecting the first link rod with the second link rod, and a gear mechanism connecting the link mechanism with the driving assembly, the gear mechanism comprising a first gear rotatably mounted on the support base and a second gear rotatably mounted on the support base, the first gear and the second gear being engaged, the first gear and/or the second gear being connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to rotate synchronously, the link mechanism comprising a first link rod fixedly connected with the first gear, a first link rod rotatably connecting a first end of the first link rod with a first end of the first link rod, a second gear rotatably connecting a second end of the first link rod with a second end of the first link rod, a second gear fixedly connected with a second end of the second link rod, a second link rod of equal length, a second link rod rotatably connecting a second end of the second link rod with a second end of the second link rod, a second link rod of equal length, and a second link rod of equal length.|5. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions of claim 4, wherein the driving assembly comprises a first driving shaft rotatably disposed on the supporting seat, a second driving shaft rotatably disposed on the supporting seat, a driving motor fixedly mounted on the supporting seat, a first synchronous pulley fixedly sleeved on the first driving shaft, a second synchronous pulley fixedly sleeved on the second driving shaft, a third synchronous pulley fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous pulley, the second synchronous pulley and the third synchronous pulley, wherein the driving motor is electrically connected with the controller.|6. A leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 3, wherein a pressure sensor for detecting leaching liquid pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.|7. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions of claim 1, wherein the leaching assembly further comprises a first mesh plate disposed in a leaching chamber within the leaching column and a first filter screen laid on the mesh plate, the silicate rock powder in the leaching column forming a columnar rock mass, a bottom end of the columnar rock mass being supported on the first mesh plate.|8. The leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 1, wherein the incubator device comprises an incubator with a constant temperature cavity inside, a refrigerator arranged on the incubator to selectively open or close the constant temperature cavity, a refrigerator arranged inside the incubator to realize temperature regulation in the constant temperature cavity, and an air circulation and heating mechanism arranged inside the incubator, wherein the air circulation and heating mechanism can accelerate air circulation flow in the constant temperature cavity and heat air in the constant temperature cavity, the controller can control the refrigerator and the air circulation and heating mechanism to work according to humidity and temperature detected by the temperature and humidity sensor, and the temperature in the constant temperature cavity is regulated so as to keep the temperature in the constant temperature cavity within a preset temperature range of 0-25 ℃.|9. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 8, wherein the air circulation and heat supply mechanism comprises a circulation air duct arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air duct, an air return pipe communicated with an air return opening of the circulation air duct, a heating assembly arranged in the circulation air duct, and a circulation fan arranged in the circulation air duct, and the heating assembly comprises a plurality of heating pipes which are transversely arranged.|10. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to any one of claims 2 to 6, wherein the spray assembly comprises a spray head connected to the infusion tube and a spray bracket for supporting the spray head on the support frame and/or at the top end of the leaching column, the spray bracket being detachably connected to the support frame and/or the leaching column. (CN121454002)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction treatment, and particularly relates to leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions.|BACKGROUND ART|[0002] The saline-alkali soil has the problems of deterioration of physical and chemical properties of soil, insufficient nutrient supply, limited plant growth and the like due to high salt content and strong alkalinity.|[0003] The conventional saline-alkali soil improvement methods comprise salt removal, salt pressing, organic fertilizer application, chemical modifier application and the like, but the methods have the defects of slow effect, high cost, high environmental risk or difficult long-term maintenance of improvement effect and the like. In recent years, mineral fertilizers have been greatly developed in the aspect of saline-alkali soil improvement, silicate minerals are utilized for weathering to release nutrient elements such as calcium, magnesium, potassium, phosphorus and the like, carbonate minerals are formed by reaction with atmospheric carbon dioxide, and research on soil improvement, nutrient supplementation, carbon fixation and sink increase is increasingly paid attention to. However, the existing research is still imperfect in simulating leaching and chemical weathering rules of silicate minerals under the conditions of natural precipitation and soil temperature and humidity, and lacks experimental verification and model support of a system. In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device:| (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition; | (2) Only is carried out at room temperature, lacks heating and temperature control functions, and cannot reflect the change of the real soil under the temperature and humidity conditions. |[0004] The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain. Therefore, development of a chemical weathering leaching experimental device capable of simulating silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment is needed to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners and novel mineral fertilizers.|DISCLOSURE|Disclosure of Invention|[0005] Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.|[0006] In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:| The temperature control device comprises a support frame and an incubator device arranged on the support frame; | The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; | a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; | a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and |And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.|[0007] Further, the rainfall simulation device comprises a spraying component arranged at the open top of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying component with a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, wherein the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the driving device, the first valve and the second valve can be controlled to work and are respectively and electrically connected with the controller.|[0008] Further, the injection pump mechanism comprises an injection cylinder, a first piston, a second piston, a push-pull rod, a first linkage rod, a sleeve and a second linkage rod, wherein the two ends of the injection cylinder are respectively in an opening shape, the first piston is arranged in the injection cylinder in a sliding mode, the second piston is arranged in the injection cylinder in a sliding mode, the push-pull rod is used for driving the first piston to move along the axial direction of the injection cylinder, the first linkage rod is connected with one end, far away from the first piston, of the push-pull rod, the sleeve is used for driving the second piston to move along the axial direction of the injection cylinder, the second linkage rod is connected with one end, far away from the second piston, of the sleeve, a first sliding hole is formed in the second piston, the outer peripheral surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve can be sleeved on the push-pull rod in an axial sliding mode, and the first linkage rod and the second linkage rod are respectively connected with the driving device.|[0009] Further, the driving device comprises a driving assembly, a connecting rod mechanism connecting the first linkage rod with the second linkage rod, and a gear mechanism connecting the connecting rod mechanism with the driving assembly, wherein the gear mechanism comprises a first gear rotatably installed on the supporting seat and a second gear rotatably installed on the supporting seat, the first gear is meshed with the second gear, the first gear and/or the second gear are/is connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to synchronously rotate, the connecting rod mechanism comprises a first driving rod fixedly connected with the first gear, a first connecting rod rotatably connecting the first end of the first driving rod with the first end of the first linkage rod, a second connecting rod rotatably connecting the second end of the first driving rod with the first end of the second linkage rod, a second driving rod fixedly connected with the second gear, a second connecting rod fixedly connected with the second end of the second driving rod, a second connecting rod fixedly connected with the second end of the second connecting rod, a second connecting rod with the second connecting rod, and a first connecting rod with the second connecting rod, and a second connecting rod with the second connecting rod, and the connecting rod with the second connecting rod with the first connecting rod and the second connecting rod with the second connecting rod.|[0010] Further, the driving assembly comprises a first driving shaft arranged on the supporting seat in a rotating mode, a second driving shaft arranged on the supporting seat in a rotating mode, a driving motor fixedly installed on the supporting seat, a first synchronous belt wheel fixedly sleeved on the first driving shaft, a second synchronous belt wheel fixedly sleeved on the second driving shaft, a third synchronous belt wheel fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous belt wheel, the second synchronous belt wheel and the third synchronous belt wheel, wherein the driving motor is electrically connected with the controller.|[0011] Further, a pressure sensor for detecting the leaching solution pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.|[0012] Further, the leaching assembly further comprises a first mesh plate arranged in a leaching cavity in the leaching column and a first filter screen paved on the mesh plate, silicate rock powder in the leaching column forms a columnar rock body, and the bottom end of the columnar rock body is supported on the first mesh plate.|[0013] Further, the incubator device includes the incubator that inside was equipped with the constant temperature chamber, set up in on the incubator in order to open or close selectively the chamber door in constant temperature chamber, set up in inside in order to realize the refrigerator of constant temperature intracavity temperature regulation of incubator, and set up in inside air cycle and the heating mechanism of incubator, air cycle and the heating mechanism can be accelerated air cycle flow in the constant temperature chamber, and heat air in the constant temperature chamber, the controller can be according to humidity and the temperature control that temperature and humidity sensor detected the refrigerator air cycle and the heating mechanism work, adjust the temperature in the constant temperature chamber, so that the temperature in the constant temperature chamber keeps in the preset temperature range of 0 ℃ to 25 ℃.|[0014] Further, the air circulation and heat supply mechanism comprises a circulation air channel arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air channel, an air return pipe communicated with an air return port of the circulation air channel, a heating component arranged in the circulation air channel and a circulation fan arranged in the circulation air channel, wherein the heating component comprises a plurality of heating pipes which are transversely arranged.|[0015] Further, the spraying assembly comprises a spray head connected with the infusion tube and a spraying support for supporting the spray head on the support frame and/or at the top end of the leaching column, and the spraying support is detachably connected with the support frame and/or the leaching column.|[0016] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:| According to the leaching equipment for simulating chemical weathering under the natural temperature and humidity conditions of silicate rock powder, which is disclosed by the embodiment of the invention, the actual natural rainfall and the natural saline-alkali soil temperature and humidity conditions can be simulated, and mineral chemical weathering of the precipitation amount is simulated according to the actual temperature and humidity of the saline-alkali soil, so that the chemical weathering process of silicate minerals in the natural environment of the saline-alkali soil is simulated truly, the true accuracy of the silicate mineral chemical weathering experimental result is improved, and the reliable weathering reaction, salt replacement and carbon fixing process data of the silicate minerals in the saline-alkali soil are obtained, so that scientific basis and experimental support are provided for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers. |DRAWINGS DESCRIPTION|[0017] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.|[0018] FIG. 1 is a schematic diagram of a three-dimensional structure of leaching equipment simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions;| FIG. 2 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; | FIG. 3 is a schematic top view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; | FIG. 4 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; | FIG. 5 is an assembly diagram of a rainfall simulation device and a driving device according to an embodiment of the present invention in a first working state; | FIG. 6 is a schematic cross-sectional view of the structure shown in FIG. 5; | fig. 7 is an assembly diagram of the rainfall simulation device and the driving device provided by the embodiment of the invention in a second working state; | FIG. 8 is a schematic top view of the structure shown in FIG. 7; | FIG. 9 is a schematic cross-sectional view of the structure shown in FIG. 7; | Fig. 10 is a schematic perspective view of a leaching assembly according to an embodiment of the present invention; | FIG. 11 is a schematic cross-sectional view of a leaching assembly according to an embodiment of the present invention; | FIG. 12 is an exploded view of a leaching assembly provided by an embodiment of the present invention; | FIG. 13 is a schematic perspective view of an incubator assembly according to an embodiment of the present invention; | Fig. 14 is a schematic cross-sectional structure of an incubator assembly according to an embodiment of the present invention. |[0019] Wherein, each reference sign in the figure:| 1-temperature control device, 11-supporting frame, 12-incubator device, 121-incubator, 122-oven door, 123-refrigerator, 124-air circulation and heat supply mechanism, 1241-circulation air duct, 1242-muffler, 1243-heating assembly, 1244-circulation fan, 1245-air inlet pipe, 125-mounting hole and 126-observation window; | 2-leaching components, 21-leaching columns, 22-liquid collecting containers, 23-liquid discharge pipes, 24-first mesh plates, 25-first filter screens, 26-second filter screens and 27-second mesh plates; | 3-a rainfall simulation device, 31-a spray assembly, 311-a spray head, 312-a spray bracket, 32-a syringe pump mechanism, 321-a syringe, 322-a first piston, 323-a second piston, 324-a push-pull rod, 325-a first linkage rod, 326-a sleeve, 327-a second linkage rod, 33-a transfusion tube, 34-a water inlet tube and 35-a supporting seat; | 4-drive means, 41-drive assembly, 411-first drive shaft, 412-second drive shaft, 413-drive motor, 414-first timing pulley, 415-second timing pulley, 416-third timing pulley, 417-timing belt, 418-motor shaft, 42-link mechanism, 421-first drive rod, 422-first link, 423-second link, 424-second drive rod, 425-third link, 426-fourth link, 43-gear mechanism, 431-first gear, 432-second gear; | 5-fixed support, 6-bolt piece, 7-liquid storage space, 8-columnar rock mass and 9-controller. |INVENTION MODE|Detailed Description|[0020] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0021] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first," "second," and "third" may explicitly or implicitly include one or more such features. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.|[0022] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.|[0023] Referring to fig. 1 to 14, a description will now be given of an leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention. Referring to fig. 1, fig. 2, fig. 3 and fig. 4 in combination, the leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions provided by the embodiment of the invention comprises a temperature control device 1, a leaching assembly 2, a rainfall simulation device 3, a temperature and humidity sensor and a controller 9, wherein the temperature control device 1 comprises a support frame 11 and a constant temperature box device 12 arranged on the support frame 11. The leaching assembly 2 comprises a leaching column 21 arranged in the incubator device 12 and a liquid collecting container 22 arranged below the leaching column 21, wherein two axial ends of the leaching column 21 respectively extend out of the incubator device 12, the top end of the leaching column 21 is open, and a liquid discharging pipe 23 communicated with the liquid collecting container 22 is arranged at the bottom end of the leaching column 21. Wherein, the leaching column 21 is a column-shaped leaching container made of high-temperature resistant transparent plastic or high-temperature resistant transparent organic glass. The rainfall simulation device 3 is used for simulating rainfall so that the leaching solution can uniformly flow into silicate rock powder in the leaching column 21 through the top end opening of the leaching column 21. The temperature and humidity sensor is used for detecting the temperature and humidity of silicate rock powder in the leaching column 21 in real time, and a probe of the temperature and humidity sensor is inserted into the leaching column 21. It should be noted that, the temperature and humidity sensor is implemented by adopting the prior art, and its working principle and structure are well known to those skilled in the art, and are not described herein. The controller 9 is used for controlling the rainfall simulation device 3 and the incubator device 12 to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of the silicate rock powder in the leaching column 21 is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column 21 is maintained at 30-80%. It should be noted that the controller 9 may be, but is not limited to, a programmable logic controller.|[0024] The basic working principle of the leaching equipment for simulating chemical weathering of silicate rock powder under the natural temperature and humidity condition is that silicate rock is crushed into silicate rock powder with the particle size of 0.1 micron, the silicate rock powder and a certain amount of saline-alkali soil are uniformly mixed and filled in a leaching column 21 of a leaching assembly 2, and a rainfall simulation device 3 is arranged at the opening at the top end of the leaching column 21. The simulated rainfall device 3 carries out real simulated rainfall characteristics on the leaching solution, so that the leaching solution can flow into the silicate rock powder in the leaching column 21 through the opening at the top end of the leaching column 21, the silicate rock powder in the leaching column 21 can be uniformly leached, disturbance on the silicate rock powder in the leaching column 21 is reduced, leaching efficiency and leaching effect of the silicate rock powder in the leaching column 21 are improved, and accuracy of silicate mineral chemical weathering experimental results is improved. In addition, during leaching, the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, and after the leaching solution permeates the silicate rock powder in the leaching column 21, the leaching solution is drained into the liquid collecting container 22 through the liquid drain pipe 23 at the bottom end of the leaching column 21. And, in the whole process of the chemical weathering experiment, the temperature in the incubator device 1 and the humidity in the leaching column 21 are detected in real time through the temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is less than 0 ℃, the controller 9 controls the heating component in the incubator device 1 to heat and work until the temperature in the incubator device 1 reaches 25 ℃, and the controller 9 controls the heating component in the incubator device 1 to stop heating and work. When the temperature in the oven apparatus 1 is greater than 25 ℃, the controller 9 controls the refrigerator in the oven apparatus 1 to operate until the temperature in the oven apparatus 1 reaches 25 ℃, and the controller 9 controls the refrigerator in the oven apparatus 1 to stop the cooling operation. The circulation is such that the temperature in the oven apparatus 1 is controlled within a preset temperature range of 0 to 25 ℃, thereby making the silicate rock powder in the leaching column 21 subjected to the chemical weathering simulation experiment under the temperature condition of 0 to 25 ℃. Of course, the controller 9 may also control the operation of the heating element and/or the refrigerator in the incubator apparatus 1 so that the temperature in the incubator apparatus 1 is stabilized at any one of the preset temperature values between 0 ℃ and 25 ℃ and so that the silicate powder in the leaching column 21 is subjected to chemical weathering simulation test under a specific temperature condition (e.g., 5 ℃, 10 ℃, 15 ℃, 20 ℃,25 ℃ or the like) between 0 ℃ and 25 ℃. Meanwhile, when the humidity in the leaching column 21 is less than 30%, the controller 9 controls the rainfall simulation device 3 to work, so that the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, until the humidity in the leaching column 21 reaches 80%, the controller 9 controls the rainfall simulation device 3 to stop working, and the circulation is performed in such a way that the humidity in the leaching column 21 is controlled within a preset humidity range of 30-80%, and thus chemical weathering simulation experiments are performed on the silicate rock powder in the leaching column 21 under a humidity condition of 30-80%. Therefore, the method can simulate the actual natural rainfall and the natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, simulate the mineral chemical weathering of the precipitation according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and improve the true accuracy of the silicate mineral chemical weathering experimental result so as to obtain the reliable weathering reaction, salt replacement and carbon fixation process data of the silicate minerals of the saline-alkali soil, thereby being beneficial to improving the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.|[0025] Referring to fig. 2,3 and 4, in some embodiments, the rainfall simulation device 3 includes a spray assembly 31 disposed at an opening at a top end of the leaching column 21, a syringe pump mechanism 32 for drawing and pumping the leaching solution, a transfusion tube 33 connecting the spray assembly 31 and a liquid outlet port of the syringe pump mechanism 32, a water inlet pipe 34 for connecting a liquid inlet port of the syringe pump mechanism 32 with a liquid storage container, and a support seat 35 for supporting the syringe pump mechanism 32, the syringe pump mechanism 32 is fixedly mounted on the support seat 35, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further includes a driving device 4 for driving the syringe pump mechanism 32 to draw and pump the leaching solution, a first valve disposed at the liquid inlet port of the syringe pump mechanism 32 and a second valve disposed at the liquid outlet port of the syringe pump mechanism 32, the driving device 4 is disposed on the support seat 35, and the controller 9 can control the driving device 4, the first valve and the second valve to work, and the driving device 4, the first valve and the second valve are respectively electrically connected with the controller 9. It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves. By the above arrangement, the silicate rock is crushed into silicate rock powder having a particle size of 0.1 μm, the silicate rock powder is packed in the leaching column 21 of the leaching assembly 2, and the spraying assembly 31 is installed at the top end opening of the leaching column 21. When the injection pump mechanism 32 is required to be used for sucking the leaching solution from the liquid storage container under the negative pressure, the controller controls the first valve 9 to open the liquid inlet of the injection pump mechanism 32, the controller controls the second valve 10 to close the liquid outlet of the injection pump mechanism 32, the driving device 4 drives the injection pump mechanism 32 to suck the leaching solution from the liquid storage container under the negative pressure, until the leaching solution in the injection pump mechanism 32 is full, the controller controls the first valve 9 to close the liquid inlet of the injection pump mechanism 32, and the controller controls the second valve 10 to open the liquid outlet of the injection pump mechanism 32, the injection pump mechanism 32 can pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the simulated rainfall device 3 under the driving action of the driving device 4, the real rainfall simulation characteristic is realized, the uniformity of the silicate powder in the leaching column 21 is ensured, the silicate powder in the leaching column 21 is uniformly leached, the disturbance of the silicate powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate powder in the leaching column 21 are further improved, and the accuracy of silicate mineral chemical weathering experiment results is facilitated. In addition, during leaching, the leaching solution of the silicate powder in the leaching column 21 is uniformly sprayed to the leaching column 21 at a certain flow rate through the spraying assembly 31, and is drained into the liquid collecting container 22 through the drain pipe 23 at the bottom end of the leaching column 21 after penetrating the silicate powder in the leaching column 21.|[0026] Therefore, in the leaching device for simulating chemical weathering of silicate rock powder under the natural temperature and humidity conditions, when the controller controls the first valve 9 to be opened and the second valve 10 to be closed, the driving device 4 can drive the injection pump mechanism 32 to draw the leaching solution from the liquid storage container through negative pressure until the injection pump mechanism 32 draws enough leaching solution, then the controller controls the first valve 9 to be closed and the second valve 10 to be opened, the injection pump mechanism 32 can continuously pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the rainfall simulator 3 under the driving action of the driving device 4, the real rainfall simulation characteristic of the spraying assembly 31 of the rainfall simulator 3 is adopted to ensure the uniformity of the leaching solution flowing into the silicate rock powder in the leaching column 21, so that the silicate rock powder in the leaching column 21 can be uniformly leached, the disturbance of the silicate rock powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate rock powder in the leaching column 21 are improved, and the accuracy of the silicate mineral chemical weathering experiment result is improved.|[0027] Referring to fig. 2,6 and 9 in combination, in some embodiments, the syringe pump mechanism 32 includes a syringe 321, a first piston 322, a second piston 323, a push-pull rod 324, a first linkage rod 325, a sleeve 326 and a second linkage rod 327, two ends of the syringe 321 are all open, the first piston 322 and the second piston 323 are respectively slidably disposed in the syringe 321, and when the first piston 322 and the second piston 323 are respectively slid to the openings at two ends of the syringe 321, a closed liquid storage space 7 for storing the shower solution can be formed in the syringe 321, and the liquid storage capacity of the liquid storage space 7 can be preset. The push-pull rod 324 is used for driving the first piston 322 to move along the axial direction of the injection cylinder 321, the sleeve 326 is used for driving the second piston 323 to move along the axial direction of the injection cylinder 321, and when the first piston 322 and the second piston 323 move away from each other along the axial direction of the injection cylinder 321, the solution can be pumped from the liquid storage container through the injection pump mechanism 32, and the pumped solution can be stored in the closed liquid storage space 7 between the first piston 322 and the second piston 323. When the first piston 322 and the second piston 323 move closer to each other in the axial direction of the syringe 321, the shower solution in the solution storage space 7 can be continuously pumped to the shower assembly 31 of the rainfall simulation device 3 by the syringe pump mechanism 32. The first linkage rod 325 is connected with one end of the push-pull rod 324 far away from the first piston 322, the second linkage rod 327 is connected with one end of the sleeve 326 far away from the second piston 323, the first linkage rod 325 and the second linkage rod 327 are respectively connected with the driving device 4, a first sliding hole for the push-pull rod 324 to pass through is arranged on the second piston 323, the outer peripheral surface of the push-pull rod 324 is in interference contact with the inner hole wall of the first sliding hole, and the sleeve 326 can be sleeved on the push-pull rod 324 in an axial sliding manner. When the driving device 4 drives the first linkage rod 325 and the second linkage rod 327, the sleeve 326 is sleeved on the push-pull rod 324 in a sliding manner along the axial direction, so that the first piston 322 and the second piston 323 can move towards or away from each other along the axial direction of the injection cylinder 321. It should be noted that, the liquid inlet port and the liquid outlet port are both disposed on the syringe 321, and the liquid inlet port and the liquid outlet port are respectively communicated with the liquid storage space 7.|[0028] Referring to fig. 4, 5, 7 and 8 in combination, in some embodiments, the driving device 4 includes a driving assembly 41, a link mechanism 42 and a gear mechanism 43, the link mechanism 42 is used to connect the first link lever 325 with the second link lever 327, the gear mechanism 43 is used to connect the link mechanism 42 with the driving assembly 41, the gear mechanism 43 includes a first gear 431 rotatably mounted on the support seat 35 and a second gear 432 rotatably mounted on the support seat 35, the first gear 431 and the second gear 432 are the same in size and structure, the first gear 431 and the second gear 432 mesh, the first gear 431 and the second gear 432 are connected with the driving assembly 41, and one gear of the first gear 431 and the second gear 432 may be connected with the driving assembly 41, so that the driving assembly 41 can drive the first gear 431 and the second gear 432 to rotate synchronously. The link mechanism 42 includes a first driving lever 421 fixedly coupled to a first gear 431, a first link 422 rotatably coupling a first end of the first driving lever 421 with a first end of a first link lever 325, a second link 423 rotatably coupling a second end of the first driving lever 421 with a first end of a second link lever 327, a second driving lever 424 fixedly coupled to a second gear 432, a third link 425 rotatably coupling a first end of the second driving lever 424 with a second end of the first link lever 325, a fourth link 426 rotatably coupling a second end of the second driving lever 424 with a first end of the second link lever 327, the lengths of the first link 422, the second link 423, the third link 425, and the fourth link 426 being equal, the length of the first link lever 325 being equal to the length of the second link lever 327, and the length of the first driving lever 421 being equal to the length of the second link lever 424. It should be noted that, two ends of the first link 422 are respectively rotatably connected to the first end of the first driving rod 421 and the first end of the first linkage rod 325 through a pivot, and two ends of the second link 423 are respectively rotatably connected to the second end of the first driving rod 421 and the second end of the first linkage rod 325 through a pivot. Through the above structure, the driving assembly 41 can synchronously drive the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321, and can improve the stability of the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321. In addition, the connecting rod mechanism 42 is driven by the rotation of the gear mechanism 43 to drive the first piston 322 and the second piston 323 to move close to each other along the axial direction of the injection cylinder 321, and the speed of the injection pump mechanism 32 for pumping the leaching solution can be controlled by controlling the rotation speed of the first gear 431 and/or the second gear 432, so that the leaching rate can be controlled and regulated according to the leaching experiment requirement.|[0029] Referring to fig. 4, 5 and 7, in some embodiments, the driving assembly 41 includes a first driving shaft 411, a second driving shaft 412, a driving motor 413, a first synchronous belt 417 wheel 414, a second synchronous belt 417 wheel 415, a third synchronous belt 417 wheel 416 and a synchronous belt 417, the first driving shaft 411 and the second driving shaft 412 are respectively rotatably disposed on the supporting seat 35, the driving motor 413 is fixedly mounted on the supporting seat 35, the first synchronous belt 417 wheel 414 is fixedly sleeved on the first driving shaft 411, the second synchronous belt 417 wheel 415 is fixedly sleeved on the second driving shaft 412, the third synchronous belt 417 wheel 416 is fixedly sleeved on a motor shaft 418 of the driving motor 413, and the synchronous belt 417 connects the first synchronous belt 417 wheel 414, the second synchronous belt 417 wheel 415 and the third synchronous belt 417 wheel 416, and the driving motor 413 is electrically connected with the controller. Through the above structure arrangement, under the driving action of the driving motor 413, the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 synchronously rotate, so as to drive the gear mechanism 43 to rotate, and the gear mechanism 43 drives the first piston 322 and the second piston 323 to move close to or far away from each other along the axial direction of the injection cylinder 321 through the link mechanism 42, so that the injection pump mechanism 32 can finish the action of drawing and pumping the shower solution.|[0030] Referring to fig. 2, 4 and 5, in some embodiments, the first gear 431 is fixedly sleeved on the first driving shaft 411, the second gear 432 is fixedly sleeved on the second driving shaft 412, and the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are arranged in an isosceles triangle, so that the distance between the first driving shaft 411 and the second driving shaft 412, the distance between the first driving shaft 411 and the motor shaft 418 of the driving motor 413, and the distance between the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are all equal. By the above arrangement, the stability of the movement of the first piston 322 and the second piston 323 in the axial direction of the syringe 321 toward each other or away from each other can be improved.|[0031] In some embodiments, a pressure sensor for detecting leaching liquid pressure inside the syringe 321 is disposed in the syringe 321, and the pressure sensor is electrically connected to the controller. The controller can control the rotation speed of the driving motor 413 to control the rotation speed of the first gear 431 and/or the second gear 432 according to the pressure detected by the pressure sensor, so as to control the speed of the injection pump mechanism 32 for pumping the leaching solution, thereby being convenient for controlling and adjusting the leaching rate according to the leaching experiment requirement.|[0032] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a first mesh plate 24 disposed in the leaching chamber in the leaching column 21 and a first filter screen 25 laid on the mesh plate, silicate rock powder in the leaching column 21 forms a columnar rock body 8, and a bottom end of the columnar rock body 8 is supported on the first mesh plate 24. Through the structure setting, through adopting the first mesh board 24 that plastics or metal etc. made to the silicate rock powder in the leaching column 21 to form column rock mass 8 bottom formation support, the leaching solution after the rethread first filter screen 25 on the first mesh board 24 filters, can prevent effectively that the silicate rock powder in the leaching column 21 from forming column rock mass 8 bottom and collapsing, ensure simultaneously that the leaching solution that liquid collecting container 22 collected does not contain silicate rock powder, be favorable to improving the accuracy of leaching experiment. The mesh size of the first screen 25 is smaller than the particle size of the silicate powder.|[0033] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a second screen 26 disposed on top of the columnar rock mass 8 and a second mesh plate 27 disposed over the second screen 26. By paving the second filter screen 26 on the top end of the columnar rock body 8 formed by silicate rock powder in the leaching column 21 and covering the second filter screen 26 with a second mesh plate 27 made of hard materials such as plastics or metals, the integrity of the top of the columnar rock body 8 is prevented from being damaged due to the fact that the concentrated impact of leaching solution water flows form a dent.|[0034] Referring to fig. 2 and 4 in combination, in some embodiments, spray assembly 31 includes a spray head 311 coupled to a fluid line 33, and a spray bracket 312 for supporting spray head 311 on support frame 1 and/or on the top of leaching column 21, spray bracket 312 being removably coupled to support frame 1 and/or leaching column 21. It should be noted that the spray head 311 may be, but is not limited to, an atomizing spray head 311. In actual operation, the speed of the driving motor 413 is controlled, and various rainfall is simulated by adopting the atomizing nozzle 311, so that silicate rock powder in the leaching column 21 forms a columnar rock body 8, and the problems that the soil column structure is damaged and the leaching speed of water is influenced due to the fact that water flow impacts to form a recess are avoided.|[0035] Referring to fig. 13 and 14 in combination, in some embodiments, the incubator apparatus 12 includes an incubator 121 having a constant temperature chamber therein, a door 122 provided on the incubator 121 to selectively open or close the constant temperature chamber, a refrigerator 123 provided inside the incubator 121 to achieve temperature adjustment in the constant temperature chamber, and an air circulation and heat supply mechanism 124 provided inside the incubator 121, the air circulation and heat supply mechanism 124 being capable of accelerating the air circulation flow in the constant temperature chamber and heating the air in the constant temperature chamber, and the controller 9 being capable of controlling the operation of the refrigerator 123, the air circulation and heat supply mechanism 124 according to the humidity and temperature detected by the temperature and humidity sensor to adjust the temperature in the constant temperature chamber so as to maintain the temperature in the constant temperature chamber within a preset temperature range of 0 to 25 ℃ or to any specific temperature value between 0 to 25 ℃. The incubator 121 is provided with a mounting hole 125 for accommodating and mounting the leaching column 21, and the outer side wall of the leaching column 21 is in airtight contact with the inner hole wall of the mounting hole 125. The door 122 is provided with a transparent observation window 126 made of high temperature resistant glass so as to observe leaching conditions in the leaching column 21 inside the incubator 121. In the whole process of chemical weathering experiment, the temperature in the incubator device 1 is detected in real time through a temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is smaller than 0 ℃, the controller 9 controls the refrigerator 123 to be closed and controls the air circulation and heat supply mechanism 124 in the heat preservation 121 to work, and the air circulation and heat supply mechanism 124 accelerates the air circulation flow in the constant temperature cavity and heats the air in the constant temperature cavity, so that the temperature in the constant temperature cavity of the incubator 121 is quickly increased until the temperature in the constant temperature cavity of the incubator 121 reaches 25 ℃, and the controller 9 controls the air circulation and heat supply mechanism 124 in the incubator device 1 to stop heating work. If the temperature in the constant temperature chamber of the incubator 121 is higher than 25 ℃, the controller 9 controls the refrigerator 123 to operate and controls the air circulation and heating mechanism 124 to stop operating, so that the temperature in the constant temperature chamber is reduced by between 0 and 25 ℃. By means of the circulation, the temperature in the heat preservation box 121 can be controlled within a preset temperature range of 0-25 ℃, so that silicate rock powder in the leaching column 21 is subjected to chemical weathering simulation experiments under the temperature condition of 0-25 ℃ to simulate actual natural rainfall and natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, mineral chemical weathering of simulated precipitation is performed according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and the actual accuracy of silicate mineral chemical weathering experiment results is improved.|[0036] Referring to fig. 13 and 14 in combination, in some embodiments, the air circulation and heat supply mechanism 124 includes a circulation duct 1241 disposed in the constant temperature chamber, an air inlet pipe 1245 connected to an air inlet of the circulation duct 1241, an air return pipe 1242 connected to an air return port of the circulation duct 1241, a heating assembly 1243 disposed in the circulation duct 1241, and a circulation fan 1244 disposed in the circulation duct 1241, the heating assembly 1243 including a plurality of heating pipes disposed transversely. When the air circulation and heat supply mechanism 124 works, air in the constant temperature cavity is led into the circulation air channel 1241 by the air inlet pipe 1245 under the action of the circulation fan 45, the air in the circulation air channel 1241 is heated by the heating component 1244 and then becomes hot air, and the hot air in the circulation air channel 1241 flows back to the constant temperature cavity by the air return pipe 1243, so that the air circulation and heat supply mechanism 124 can be used for quickly heating the air in the constant temperature cavity.|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention. (CN121454002)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction treatment, and particularly relates to leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions.|BACKGROUND ART|[0002] The saline-alkali soil has the problems of deterioration of physical and chemical properties of soil, insufficient nutrient supply, limited plant growth and the like due to high salt content and strong alkalinity.|[0003] The conventional saline-alkali soil improvement methods comprise salt removal, salt pressing, organic fertilizer application, chemical modifier application and the like, but the methods have the defects of slow effect, high cost, high environmental risk or difficult long-term maintenance of improvement effect and the like. In recent years, mineral fertilizers have been greatly developed in the aspect of saline-alkali soil improvement, silicate minerals are utilized for weathering to release nutrient elements such as calcium, magnesium, potassium, phosphorus and the like, carbonate minerals are formed by reaction with atmospheric carbon dioxide, and research on soil improvement, nutrient supplementation, carbon fixation and sink increase is increasingly paid attention to. However, the existing research is still imperfect in simulating leaching and chemical weathering rules of silicate minerals under the conditions of natural precipitation and soil temperature and humidity, and lacks experimental verification and model support of a system. In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device:| (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition; | (2) Only is carried out at room temperature, lacks heating and temperature control functions, and cannot reflect the change of the real soil under the temperature and humidity conditions. |[0004] The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain. Therefore, development of a chemical weathering leaching experimental device capable of simulating silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment is needed to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners and novel mineral fertilizers.|DISCLOSURE|Disclosure of Invention|[0005] Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.|[0006] In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:| The temperature control device comprises a support frame and an incubator device arranged on the support frame; | The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; | a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; | a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and |And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.|[0007] Further, the rainfall simulation device comprises a spraying component arranged at the open top of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying component with a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, wherein the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the driving device, the first valve and the second valve can be controlled to work and are respectively and electrically connected with the controller.|[0008] Further, the injection pump mechanism comprises an injection cylinder, a first piston, a second piston, a push-pull rod, a first linkage rod, a sleeve and a second linkage rod, wherein the two ends of the injection cylinder are respectively in an opening shape, the first piston is arranged in the injection cylinder in a sliding mode, the second piston is arranged in the injection cylinder in a sliding mode, the push-pull rod is used for driving the first piston to move along the axial direction of the injection cylinder, the first linkage rod is connected with one end, far away from the first piston, of the push-pull rod, the sleeve is used for driving the second piston to move along the axial direction of the injection cylinder, the second linkage rod is connected with one end, far away from the second piston, of the sleeve, a first sliding hole is formed in the second piston, the outer peripheral surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve can be sleeved on the push-pull rod in an axial sliding mode, and the first linkage rod and the second linkage rod are respectively connected with the driving device.|[0009] Further, the driving device comprises a driving assembly, a connecting rod mechanism connecting the first linkage rod with the second linkage rod, and a gear mechanism connecting the connecting rod mechanism with the driving assembly, wherein the gear mechanism comprises a first gear rotatably installed on the supporting seat and a second gear rotatably installed on the supporting seat, the first gear is meshed with the second gear, the first gear and/or the second gear are/is connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to synchronously rotate, the connecting rod mechanism comprises a first driving rod fixedly connected with the first gear, a first connecting rod rotatably connecting the first end of the first driving rod with the first end of the first linkage rod, a second connecting rod rotatably connecting the second end of the first driving rod with the first end of the second linkage rod, a second driving rod fixedly connected with the second gear, a second connecting rod fixedly connected with the second end of the second driving rod, a second connecting rod fixedly connected with the second end of the second connecting rod, a second connecting rod with the second connecting rod, and a first connecting rod with the second connecting rod, and a second connecting rod with the second connecting rod, and the connecting rod with the second connecting rod with the first connecting rod and the second connecting rod with the second connecting rod.|[0010] Further, the driving assembly comprises a first driving shaft arranged on the supporting seat in a rotating mode, a second driving shaft arranged on the supporting seat in a rotating mode, a driving motor fixedly installed on the supporting seat, a first synchronous belt wheel fixedly sleeved on the first driving shaft, a second synchronous belt wheel fixedly sleeved on the second driving shaft, a third synchronous belt wheel fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous belt wheel, the second synchronous belt wheel and the third synchronous belt wheel, wherein the driving motor is electrically connected with the controller.|[0011] Further, a pressure sensor for detecting the leaching solution pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.|[0012] Further, the leaching assembly further comprises a first mesh plate arranged in a leaching cavity in the leaching column and a first filter screen paved on the mesh plate, silicate rock powder in the leaching column forms a columnar rock body, and the bottom end of the columnar rock body is supported on the first mesh plate.|[0013] Further, the incubator device includes the incubator that inside was equipped with the constant temperature chamber, set up in on the incubator in order to open or close selectively the chamber door in constant temperature chamber, set up in inside in order to realize the refrigerator of constant temperature intracavity temperature regulation of incubator, and set up in inside air cycle and the heating mechanism of incubator, air cycle and the heating mechanism can be accelerated air cycle flow in the constant temperature chamber, and heat air in the constant temperature chamber, the controller can be according to humidity and the temperature control that temperature and humidity sensor detected the refrigerator air cycle and the heating mechanism work, adjust the temperature in the constant temperature chamber, so that the temperature in the constant temperature chamber keeps in the preset temperature range of 0 ℃ to 25 ℃.|[0014] Further, the air circulation and heat supply mechanism comprises a circulation air channel arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air channel, an air return pipe communicated with an air return port of the circulation air channel, a heating component arranged in the circulation air channel and a circulation fan arranged in the circulation air channel, wherein the heating component comprises a plurality of heating pipes which are transversely arranged.|[0015] Further, the spraying assembly comprises a spray head connected with the infusion tube and a spraying support for supporting the spray head on the support frame and/or at the top end of the leaching column, and the spraying support is detachably connected with the support frame and/or the leaching column.|[0016] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:| According to the leaching equipment for simulating chemical weathering under the natural temperature and humidity conditions of silicate rock powder, which is disclosed by the embodiment of the invention, the actual natural rainfall and the natural saline-alkali soil temperature and humidity conditions can be simulated, and mineral chemical weathering of the precipitation amount is simulated according to the actual temperature and humidity of the saline-alkali soil, so that the chemical weathering process of silicate minerals in the natural environment of the saline-alkali soil is simulated truly, the true accuracy of the silicate mineral chemical weathering experimental result is improved, and the reliable weathering reaction, salt replacement and carbon fixing process data of the silicate minerals in the saline-alkali soil are obtained, so that scientific basis and experimental support are provided for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers. |DRAWINGS DESCRIPTION|[0017] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.|[0018] FIG. 1 is a schematic diagram of a three-dimensional structure of leaching equipment simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions;| FIG. 2 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; | FIG. 3 is a schematic top view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; | FIG. 4 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; | FIG. 5 is an assembly diagram of a rainfall simulation device and a driving device according to an embodiment of the present invention in a first working state; | FIG. 6 is a schematic cross-sectional view of the structure shown in FIG. 5; | fig. 7 is an assembly diagram of the rainfall simulation device and the driving device provided by the embodiment of the invention in a second working state; | FIG. 8 is a schematic top view of the structure shown in FIG. 7; | FIG. 9 is a schematic cross-sectional view of the structure shown in FIG. 7; | Fig. 10 is a schematic perspective view of a leaching assembly according to an embodiment of the present invention; | FIG. 11 is a schematic cross-sectional view of a leaching assembly according to an embodiment of the present invention; | FIG. 12 is an exploded view of a leaching assembly provided by an embodiment of the present invention; | FIG. 13 is a schematic perspective view of an incubator assembly according to an embodiment of the present invention; | Fig. 14 is a schematic cross-sectional structure of an incubator assembly according to an embodiment of the present invention. |[0019] Wherein, each reference sign in the figure:| 1-temperature control device, 11-supporting frame, 12-incubator device, 121-incubator, 122-oven door, 123-refrigerator, 124-air circulation and heat supply mechanism, 1241-circulation air duct, 1242-muffler, 1243-heating assembly, 1244-circulation fan, 1245-air inlet pipe, 125-mounting hole and 126-observation window; | 2-leaching components, 21-leaching columns, 22-liquid collecting containers, 23-liquid discharge pipes, 24-first mesh plates, 25-first filter screens, 26-second filter screens and 27-second mesh plates; | 3-a rainfall simulation device, 31-a spray assembly, 311-a spray head, 312-a spray bracket, 32-a syringe pump mechanism, 321-a syringe, 322-a first piston, 323-a second piston, 324-a push-pull rod, 325-a first linkage rod, 326-a sleeve, 327-a second linkage rod, 33-a transfusion tube, 34-a water inlet tube and 35-a supporting seat; | 4-drive means, 41-drive assembly, 411-first drive shaft, 412-second drive shaft, 413-drive motor, 414-first timing pulley, 415-second timing pulley, 416-third timing pulley, 417-timing belt, 418-motor shaft, 42-link mechanism, 421-first drive rod, 422-first link, 423-second link, 424-second drive rod, 425-third link, 426-fourth link, 43-gear mechanism, 431-first gear, 432-second gear; | 5-fixed support, 6-bolt piece, 7-liquid storage space, 8-columnar rock mass and 9-controller. |INVENTION MODE|Detailed Description|[0020] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0021] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first," "second," and "third" may explicitly or implicitly include one or more such features. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.|[0022] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.|[0023] Referring to fig. 1 to 14, a description will now be given of an leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention. Referring to fig. 1, fig. 2, fig. 3 and fig. 4 in combination, the leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions provided by the embodiment of the invention comprises a temperature control device 1, a leaching assembly 2, a rainfall simulation device 3, a temperature and humidity sensor and a controller 9, wherein the temperature control device 1 comprises a support frame 11 and a constant temperature box device 12 arranged on the support frame 11. The leaching assembly 2 comprises a leaching column 21 arranged in the incubator device 12 and a liquid collecting container 22 arranged below the leaching column 21, wherein two axial ends of the leaching column 21 respectively extend out of the incubator device 12, the top end of the leaching column 21 is open, and a liquid discharging pipe 23 communicated with the liquid collecting container 22 is arranged at the bottom end of the leaching column 21. Wherein, the leaching column 21 is a column-shaped leaching container made of high-temperature resistant transparent plastic or high-temperature resistant transparent organic glass. The rainfall simulation device 3 is used for simulating rainfall so that the leaching solution can uniformly flow into silicate rock powder in the leaching column 21 through the top end opening of the leaching column 21. The temperature and humidity sensor is used for detecting the temperature and humidity of silicate rock powder in the leaching column 21 in real time, and a probe of the temperature and humidity sensor is inserted into the leaching column 21. It should be noted that, the temperature and humidity sensor is implemented by adopting the prior art, and its working principle and structure are well known to those skilled in the art, and are not described herein. The controller 9 is used for controlling the rainfall simulation device 3 and the incubator device 12 to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of the silicate rock powder in the leaching column 21 is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column 21 is maintained at 30-80%. It should be noted that the controller 9 may be, but is not limited to, a programmable logic controller.|[0024] The basic working principle of the leaching equipment for simulating chemical weathering of silicate rock powder under the natural temperature and humidity condition is that silicate rock is crushed into silicate rock powder with the particle size of 0.1 micron, the silicate rock powder and a certain amount of saline-alkali soil are uniformly mixed and filled in a leaching column 21 of a leaching assembly 2, and a rainfall simulation device 3 is arranged at the opening at the top end of the leaching column 21. The simulated rainfall device 3 carries out real simulated rainfall characteristics on the leaching solution, so that the leaching solution can flow into the silicate rock powder in the leaching column 21 through the opening at the top end of the leaching column 21, the silicate rock powder in the leaching column 21 can be uniformly leached, disturbance on the silicate rock powder in the leaching column 21 is reduced, leaching efficiency and leaching effect of the silicate rock powder in the leaching column 21 are improved, and accuracy of silicate mineral chemical weathering experimental results is improved. In addition, during leaching, the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, and after the leaching solution permeates the silicate rock powder in the leaching column 21, the leaching solution is drained into the liquid collecting container 22 through the liquid drain pipe 23 at the bottom end of the leaching column 21. And, in the whole process of the chemical weathering experiment, the temperature in the incubator device 1 and the humidity in the leaching column 21 are detected in real time through the temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is less than 0 ℃, the controller 9 controls the heating component in the incubator device 1 to heat and work until the temperature in the incubator device 1 reaches 25 ℃, and the controller 9 controls the heating component in the incubator device 1 to stop heating and work. When the temperature in the oven apparatus 1 is greater than 25 ℃, the controller 9 controls the refrigerator in the oven apparatus 1 to operate until the temperature in the oven apparatus 1 reaches 25 ℃, and the controller 9 controls the refrigerator in the oven apparatus 1 to stop the cooling operation. The circulation is such that the temperature in the oven apparatus 1 is controlled within a preset temperature range of 0 to 25 ℃, thereby making the silicate rock powder in the leaching column 21 subjected to the chemical weathering simulation experiment under the temperature condition of 0 to 25 ℃. Of course, the controller 9 may also control the operation of the heating element and/or the refrigerator in the incubator apparatus 1 so that the temperature in the incubator apparatus 1 is stabilized at any one of the preset temperature values between 0 ℃ and 25 ℃ and so that the silicate powder in the leaching column 21 is subjected to chemical weathering simulation test under a specific temperature condition (e.g., 5 ℃, 10 ℃, 15 ℃, 20 ℃,25 ℃ or the like) between 0 ℃ and 25 ℃. Meanwhile, when the humidity in the leaching column 21 is less than 30%, the controller 9 controls the rainfall simulation device 3 to work, so that the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, until the humidity in the leaching column 21 reaches 80%, the controller 9 controls the rainfall simulation device 3 to stop working, and the circulation is performed in such a way that the humidity in the leaching column 21 is controlled within a preset humidity range of 30-80%, and thus chemical weathering simulation experiments are performed on the silicate rock powder in the leaching column 21 under a humidity condition of 30-80%. Therefore, the method can simulate the actual natural rainfall and the natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, simulate the mineral chemical weathering of the precipitation according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and improve the true accuracy of the silicate mineral chemical weathering experimental result so as to obtain the reliable weathering reaction, salt replacement and carbon fixation process data of the silicate minerals of the saline-alkali soil, thereby being beneficial to improving the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.|[0025] Referring to fig. 2,3 and 4, in some embodiments, the rainfall simulation device 3 includes a spray assembly 31 disposed at an opening at a top end of the leaching column 21, a syringe pump mechanism 32 for drawing and pumping the leaching solution, a transfusion tube 33 connecting the spray assembly 31 and a liquid outlet port of the syringe pump mechanism 32, a water inlet pipe 34 for connecting a liquid inlet port of the syringe pump mechanism 32 with a liquid storage container, and a support seat 35 for supporting the syringe pump mechanism 32, the syringe pump mechanism 32 is fixedly mounted on the support seat 35, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further includes a driving device 4 for driving the syringe pump mechanism 32 to draw and pump the leaching solution, a first valve disposed at the liquid inlet port of the syringe pump mechanism 32 and a second valve disposed at the liquid outlet port of the syringe pump mechanism 32, the driving device 4 is disposed on the support seat 35, and the controller 9 can control the driving device 4, the first valve and the second valve to work, and the driving device 4, the first valve and the second valve are respectively electrically connected with the controller 9. It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves. By the above arrangement, the silicate rock is crushed into silicate rock powder having a particle size of 0.1 μm, the silicate rock powder is packed in the leaching column 21 of the leaching assembly 2, and the spraying assembly 31 is installed at the top end opening of the leaching column 21. When the injection pump mechanism 32 is required to be used for sucking the leaching solution from the liquid storage container under the negative pressure, the controller controls the first valve 9 to open the liquid inlet of the injection pump mechanism 32, the controller controls the second valve 10 to close the liquid outlet of the injection pump mechanism 32, the driving device 4 drives the injection pump mechanism 32 to suck the leaching solution from the liquid storage container under the negative pressure, until the leaching solution in the injection pump mechanism 32 is full, the controller controls the first valve 9 to close the liquid inlet of the injection pump mechanism 32, and the controller controls the second valve 10 to open the liquid outlet of the injection pump mechanism 32, the injection pump mechanism 32 can pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the simulated rainfall device 3 under the driving action of the driving device 4, the real rainfall simulation characteristic is realized, the uniformity of the silicate powder in the leaching column 21 is ensured, the silicate powder in the leaching column 21 is uniformly leached, the disturbance of the silicate powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate powder in the leaching column 21 are further improved, and the accuracy of silicate mineral chemical weathering experiment results is facilitated. In addition, during leaching, the leaching solution of the silicate powder in the leaching column 21 is uniformly sprayed to the leaching column 21 at a certain flow rate through the spraying assembly 31, and is drained into the liquid collecting container 22 through the drain pipe 23 at the bottom end of the leaching column 21 after penetrating the silicate powder in the leaching column 21.|[0026] Therefore, in the leaching device for simulating chemical weathering of silicate rock powder under the natural temperature and humidity conditions, when the controller controls the first valve 9 to be opened and the second valve 10 to be closed, the driving device 4 can drive the injection pump mechanism 32 to draw the leaching solution from the liquid storage container through negative pressure until the injection pump mechanism 32 draws enough leaching solution, then the controller controls the first valve 9 to be closed and the second valve 10 to be opened, the injection pump mechanism 32 can continuously pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the rainfall simulator 3 under the driving action of the driving device 4, the real rainfall simulation characteristic of the spraying assembly 31 of the rainfall simulator 3 is adopted to ensure the uniformity of the leaching solution flowing into the silicate rock powder in the leaching column 21, so that the silicate rock powder in the leaching column 21 can be uniformly leached, the disturbance of the silicate rock powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate rock powder in the leaching column 21 are improved, and the accuracy of the silicate mineral chemical weathering experiment result is improved.|[0027] Referring to fig. 2,6 and 9 in combination, in some embodiments, the syringe pump mechanism 32 includes a syringe 321, a first piston 322, a second piston 323, a push-pull rod 324, a first linkage rod 325, a sleeve 326 and a second linkage rod 327, two ends of the syringe 321 are all open, the first piston 322 and the second piston 323 are respectively slidably disposed in the syringe 321, and when the first piston 322 and the second piston 323 are respectively slid to the openings at two ends of the syringe 321, a closed liquid storage space 7 for storing the shower solution can be formed in the syringe 321, and the liquid storage capacity of the liquid storage space 7 can be preset. The push-pull rod 324 is used for driving the first piston 322 to move along the axial direction of the injection cylinder 321, the sleeve 326 is used for driving the second piston 323 to move along the axial direction of the injection cylinder 321, and when the first piston 322 and the second piston 323 move away from each other along the axial direction of the injection cylinder 321, the solution can be pumped from the liquid storage container through the injection pump mechanism 32, and the pumped solution can be stored in the closed liquid storage space 7 between the first piston 322 and the second piston 323. When the first piston 322 and the second piston 323 move closer to each other in the axial direction of the syringe 321, the shower solution in the solution storage space 7 can be continuously pumped to the shower assembly 31 of the rainfall simulation device 3 by the syringe pump mechanism 32. The first linkage rod 325 is connected with one end of the push-pull rod 324 far away from the first piston 322, the second linkage rod 327 is connected with one end of the sleeve 326 far away from the second piston 323, the first linkage rod 325 and the second linkage rod 327 are respectively connected with the driving device 4, a first sliding hole for the push-pull rod 324 to pass through is arranged on the second piston 323, the outer peripheral surface of the push-pull rod 324 is in interference contact with the inner hole wall of the first sliding hole, and the sleeve 326 can be sleeved on the push-pull rod 324 in an axial sliding manner. When the driving device 4 drives the first linkage rod 325 and the second linkage rod 327, the sleeve 326 is sleeved on the push-pull rod 324 in a sliding manner along the axial direction, so that the first piston 322 and the second piston 323 can move towards or away from each other along the axial direction of the injection cylinder 321. It should be noted that, the liquid inlet port and the liquid outlet port are both disposed on the syringe 321, and the liquid inlet port and the liquid outlet port are respectively communicated with the liquid storage space 7.|[0028] Referring to fig. 4, 5, 7 and 8 in combination, in some embodiments, the driving device 4 includes a driving assembly 41, a link mechanism 42 and a gear mechanism 43, the link mechanism 42 is used to connect the first link lever 325 with the second link lever 327, the gear mechanism 43 is used to connect the link mechanism 42 with the driving assembly 41, the gear mechanism 43 includes a first gear 431 rotatably mounted on the support seat 35 and a second gear 432 rotatably mounted on the support seat 35, the first gear 431 and the second gear 432 are the same in size and structure, the first gear 431 and the second gear 432 mesh, the first gear 431 and the second gear 432 are connected with the driving assembly 41, and one gear of the first gear 431 and the second gear 432 may be connected with the driving assembly 41, so that the driving assembly 41 can drive the first gear 431 and the second gear 432 to rotate synchronously. The link mechanism 42 includes a first driving lever 421 fixedly coupled to a first gear 431, a first link 422 rotatably coupling a first end of the first driving lever 421 with a first end of a first link lever 325, a second link 423 rotatably coupling a second end of the first driving lever 421 with a first end of a second link lever 327, a second driving lever 424 fixedly coupled to a second gear 432, a third link 425 rotatably coupling a first end of the second driving lever 424 with a second end of the first link lever 325, a fourth link 426 rotatably coupling a second end of the second driving lever 424 with a first end of the second link lever 327, the lengths of the first link 422, the second link 423, the third link 425, and the fourth link 426 being equal, the length of the first link lever 325 being equal to the length of the second link lever 327, and the length of the first driving lever 421 being equal to the length of the second link lever 424. It should be noted that, two ends of the first link 422 are respectively rotatably connected to the first end of the first driving rod 421 and the first end of the first linkage rod 325 through a pivot, and two ends of the second link 423 are respectively rotatably connected to the second end of the first driving rod 421 and the second end of the first linkage rod 325 through a pivot. Through the above structure, the driving assembly 41 can synchronously drive the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321, and can improve the stability of the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321. In addition, the connecting rod mechanism 42 is driven by the rotation of the gear mechanism 43 to drive the first piston 322 and the second piston 323 to move close to each other along the axial direction of the injection cylinder 321, and the speed of the injection pump mechanism 32 for pumping the leaching solution can be controlled by controlling the rotation speed of the first gear 431 and/or the second gear 432, so that the leaching rate can be controlled and regulated according to the leaching experiment requirement.|[0029] Referring to fig. 4, 5 and 7, in some embodiments, the driving assembly 41 includes a first driving shaft 411, a second driving shaft 412, a driving motor 413, a first synchronous belt 417 wheel 414, a second synchronous belt 417 wheel 415, a third synchronous belt 417 wheel 416 and a synchronous belt 417, the first driving shaft 411 and the second driving shaft 412 are respectively rotatably disposed on the supporting seat 35, the driving motor 413 is fixedly mounted on the supporting seat 35, the first synchronous belt 417 wheel 414 is fixedly sleeved on the first driving shaft 411, the second synchronous belt 417 wheel 415 is fixedly sleeved on the second driving shaft 412, the third synchronous belt 417 wheel 416 is fixedly sleeved on a motor shaft 418 of the driving motor 413, and the synchronous belt 417 connects the first synchronous belt 417 wheel 414, the second synchronous belt 417 wheel 415 and the third synchronous belt 417 wheel 416, and the driving motor 413 is electrically connected with the controller. Through the above structure arrangement, under the driving action of the driving motor 413, the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 synchronously rotate, so as to drive the gear mechanism 43 to rotate, and the gear mechanism 43 drives the first piston 322 and the second piston 323 to move close to or far away from each other along the axial direction of the injection cylinder 321 through the link mechanism 42, so that the injection pump mechanism 32 can finish the action of drawing and pumping the shower solution.|[0030] Referring to fig. 2, 4 and 5, in some embodiments, the first gear 431 is fixedly sleeved on the first driving shaft 411, the second gear 432 is fixedly sleeved on the second driving shaft 412, and the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are arranged in an isosceles triangle, so that the distance between the first driving shaft 411 and the second driving shaft 412, the distance between the first driving shaft 411 and the motor shaft 418 of the driving motor 413, and the distance between the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are all equal. By the above arrangement, the stability of the movement of the first piston 322 and the second piston 323 in the axial direction of the syringe 321 toward each other or away from each other can be improved.|[0031] In some embodiments, a pressure sensor for detecting leaching liquid pressure inside the syringe 321 is disposed in the syringe 321, and the pressure sensor is electrically connected to the controller. The controller can control the rotation speed of the driving motor 413 to control the rotation speed of the first gear 431 and/or the second gear 432 according to the pressure detected by the pressure sensor, so as to control the speed of the injection pump mechanism 32 for pumping the leaching solution, thereby being convenient for controlling and adjusting the leaching rate according to the leaching experiment requirement.|[0032] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a first mesh plate 24 disposed in the leaching chamber in the leaching column 21 and a first filter screen 25 laid on the mesh plate, silicate rock powder in the leaching column 21 forms a columnar rock body 8, and a bottom end of the columnar rock body 8 is supported on the first mesh plate 24. Through the structure setting, through adopting the first mesh board 24 that plastics or metal etc. made to the silicate rock powder in the leaching column 21 to form column rock mass 8 bottom formation support, the leaching solution after the rethread first filter screen 25 on the first mesh board 24 filters, can prevent effectively that the silicate rock powder in the leaching column 21 from forming column rock mass 8 bottom and collapsing, ensure simultaneously that the leaching solution that liquid collecting container 22 collected does not contain silicate rock powder, be favorable to improving the accuracy of leaching experiment. The mesh size of the first screen 25 is smaller than the particle size of the silicate powder.|[0033] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a second screen 26 disposed on top of the columnar rock mass 8 and a second mesh plate 27 disposed over the second screen 26. By paving the second filter screen 26 on the top end of the columnar rock body 8 formed by silicate rock powder in the leaching column 21 and covering the second filter screen 26 with a second mesh plate 27 made of hard materials such as plastics or metals, the integrity of the top of the columnar rock body 8 is prevented from being damaged due to the fact that the concentrated impact of leaching solution water flows form a dent.|[0034] Referring to fig. 2 and 4 in combination, in some embodiments, spray assembly 31 includes a spray head 311 coupled to a fluid line 33, and a spray bracket 312 for supporting spray head 311 on support frame 1 and/or on the top of leaching column 21, spray bracket 312 being removably coupled to support frame 1 and/or leaching column 21. It should be noted that the spray head 311 may be, but is not limited to, an atomizing spray head 311. In actual operation, the speed of the driving motor 413 is controlled, and various rainfall is simulated by adopting the atomizing nozzle 311, so that silicate rock powder in the leaching column 21 forms a columnar rock body 8, and the problems that the soil column structure is damaged and the leaching speed of water is influenced due to the fact that water flow impacts to form a recess are avoided.|[0035] Referring to fig. 13 and 14 in combination, in some embodiments, the incubator apparatus 12 includes an incubator 121 having a constant temperature chamber therein, a door 122 provided on the incubator 121 to selectively open or close the constant temperature chamber, a refrigerator 123 provided inside the incubator 121 to achieve temperature adjustment in the constant temperature chamber, and an air circulation and heat supply mechanism 124 provided inside the incubator 121, the air circulation and heat supply mechanism 124 being capable of accelerating the air circulation flow in the constant temperature chamber and heating the air in the constant temperature chamber, and the controller 9 being capable of controlling the operation of the refrigerator 123, the air circulation and heat supply mechanism 124 according to the humidity and temperature detected by the temperature and humidity sensor to adjust the temperature in the constant temperature chamber so as to maintain the temperature in the constant temperature chamber within a preset temperature range of 0 to 25 ℃ or to any specific temperature value between 0 to 25 ℃. The incubator 121 is provided with a mounting hole 125 for accommodating and mounting the leaching column 21, and the outer side wall of the leaching column 21 is in airtight contact with the inner hole wall of the mounting hole 125. The door 122 is provided with a transparent observation window 126 made of high temperature resistant glass so as to observe leaching conditions in the leaching column 21 inside the incubator 121. In the whole process of chemical weathering experiment, the temperature in the incubator device 1 is detected in real time through a temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is smaller than 0 ℃, the controller 9 controls the refrigerator 123 to be closed and controls the air circulation and heat supply mechanism 124 in the heat preservation 121 to work, and the air circulation and heat supply mechanism 124 accelerates the air circulation flow in the constant temperature cavity and heats the air in the constant temperature cavity, so that the temperature in the constant temperature cavity of the incubator 121 is quickly increased until the temperature in the constant temperature cavity of the incubator 121 reaches 25 ℃, and the controller 9 controls the air circulation and heat supply mechanism 124 in the incubator device 1 to stop heating work. If the temperature in the constant temperature chamber of the incubator 121 is higher than 25 ℃, the controller 9 controls the refrigerator 123 to operate and controls the air circulation and heating mechanism 124 to stop operating, so that the temperature in the constant temperature chamber is reduced by between 0 and 25 ℃. By means of the circulation, the temperature in the heat preservation box 121 can be controlled within a preset temperature range of 0-25 ℃, so that silicate rock powder in the leaching column 21 is subjected to chemical weathering simulation experiments under the temperature condition of 0-25 ℃ to simulate actual natural rainfall and natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, mineral chemical weathering of simulated precipitation is performed according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and the actual accuracy of silicate mineral chemical weathering experiment results is improved.|[0036] Referring to fig. 13 and 14 in combination, in some embodiments, the air circulation and heat supply mechanism 124 includes a circulation duct 1241 disposed in the constant temperature chamber, an air inlet pipe 1245 connected to an air inlet of the circulation duct 1241, an air return pipe 1242 connected to an air return port of the circulation duct 1241, a heating assembly 1243 disposed in the circulation duct 1241, and a circulation fan 1244 disposed in the circulation duct 1241, the heating assembly 1243 including a plurality of heating pipes disposed transversely. When the air circulation and heat supply mechanism 124 works, air in the constant temperature cavity is led into the circulation air channel 1241 by the air inlet pipe 1245 under the action of the circulation fan 45, the air in the circulation air channel 1241 is heated by the heating component 1244 and then becomes hot air, and the hot air in the circulation air channel 1241 flows back to the constant temperature cavity by the air return pipe 1243, so that the air circulation and heat supply mechanism 124 can be used for quickly heating the air in the constant temperature cavity.|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention. Family Number|(117662153)|117662153|Abstract|(CN121454002 A)|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions , and belongs to the technical fields of rock weathering and carbon sequestration enhancement , mineral fertilizer development and saline soil improvement and treatment . The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions . The leaching equipment comprises a temperature control device , a leaching assembly , a rainfall simulation device , a temperature and humidity sensor and a controller , wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame . The leaching assembly comprises a leaching column arranged in the constant - temperature box device and a liquid collecting container arranged below the leaching column . The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline - alkali soil ; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners , novel mineral fertilizers and saline - alkali soil improvement . |CPC codes|(CN121454002 A)|G01N - 033/00 |G01N - 033/24 |IPC codes|(CN121454002 A)|G01N - 033/00 |G01N - 033/24 |Title|(CN121454002 A)|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions | Analysis of biological materials G01N-033/00|G01N-033/00/98|G01N-033/24 G01N-033/00|G01N-033/00/98|G01N-033/24 G01N-033/00|G01N-033/24 G01N-033/00|G01N-033/24 PENDING (CN121454002)|PENDING ALIVE (CN121454002)|ALIVE (CN121454002)|LEGAL DETAILS FOR CN121454002|Actual or expected expiration date=2045-11-20|Legal state=ALIVE|Status=PENDING|Event publication date=2025-11-20|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511707827|Application date=2025-11-20|Standardized application number=2025CN-1707827|Event publication date=2026-02-03|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121454002|Publication stage code=A|Publication date=2026-02-03|Standardized publication number=CN121454002|Event publication date=2026-02-03|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2026-02-24|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121454002)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKc0O21wABuVOlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080718408&ekey=2075&xpn=CN121454002&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=G2LF5CjifuL%252Fkpe3oMQTWZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121454002)|CN (CN121454002)|NAME=LANZHOU UNIVERSITY , COUNTRY=CN (CN121454002)|NAME=HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=41028 (CN121454002)|CN (CN121454002)|NAME=ZHANG JIETANG, COUNTRY=CN |NAME=LI XINGYUAN|NAME=GOU XIAOHUA 0 1 Titre: (CN121454002)|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions Résumé: (CN121454002)|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of rock weathering and carbon sequestration enhancement, mineral fertilizer development and saline soil improvement and treatment. The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions. The leaching equipment comprises a temperature control device, a leaching assembly, a rainfall simulation device, a temperature and humidity sensor and a controller, wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame. The leaching assembly comprises a leaching column arranged in the constant-temperature box device and a liquid collecting container arranged below the leaching column. The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline-alkali soil; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners, novel mineral fertilizers and saline-alkali soil improvement. 60 Abstract gpt-4o-mini yes The article describes leaching equipment designed to simulate chemical weathering of silicate rocks, which is directly related to enhanced weathering and carbon sequestration.
61 CN202311567112 US18/408,544|JP2024000943|CN202311567112 US12595419|JP7719532|JP2025084647|US20250163330|CN117358724 108074209 US12595419 B2 2026-04-07 [US12595419]|US20250163330 A1 2025-05-22 [US20250163330]|JP7719532 B2 2025-08-06 [JP7719532]|JP2025084647 A 2025-06-03 [JP2025084647]|CN117358724 A 2024-01-09 [CN117358724] 2023-11-22 2024-01-09|2024-01-09|2023-11-22 2026-04-07|2025-08-06|2025-06-03|2025-05-22|2024-01-09 (US12595419)|2026-04-07|(JP7719532)|2025-08-06| (US12595419)|2044-08-31|(JP7719532)|2044-01-09|(CN117358724)|2043-11-22 (US12595419)|Household perishable garbage treatment equipment and use method thereof (US12595419)|A household perishable garbage treatment equipment and a use method thereof are provided, relating to the technical field of environmental engineering. The equipment includes a crushing unit, a pyrolysis unit, and a condensation and washing unit. Perishable garbage is crushed by the crushing unit, then the crushed perishable garbage is pyrolyzed into pyrolytic biochar by the pyrolysis unit, and gas produced in the pyrolysis process is condensed and collected by the condensation and washing unit. The household perishable garbage treatment equipment and the use method thereof can effectively treat perishable garbage on the spot, reduce the collection and treatment cost required by traditional perishable garbage treatment modes, achieve carbon sequestration and resource utilization of products, and have significant economic, ecological and social benefits. WENZHOU UNIVERSITY (US12595419)|Wenzhou University ([CN])|(US20250163330)|Wenzhou University ([CN])|(JP7719532)|WENZHOU UNIV|(JP2025084647)|WENZHOU UNIV|(CN117358724)|WENZHOU UNIVERSITY ([CN]) ZHENG XIANGYONG|MA PING|ZHAO MIN|ZHU WENCONG|JIANG SHUNFENG|WANG ZHIQUAN|JIN HUACHANG|WU SUQING|JIN ZHAN|BEI KE|XU BENTUO|KONG HAINAN (US12595419)|Zheng Xiangyong|Ma Ping|Zhao Min|Zhu Wencong|Jiang Shunfeng|Wang Zhiquan|Jin Huachang|Wu Suqing|Jin Zhan|Bei Ke|Xu Bentuo|Kong Hainan|(US20250163330)|ZHENG Xiangyong|MA Ping|ZHAO Min|ZHU Wencong|JIANG Shunfeng|WANG Zhiquan|JIN Huachang|WU Suqing|JIN Zhan|BEI Ke|XU Bentuo|KONG Hainan (US12595419)|CM Law LLP|Klinger Robert C.|(JP7719532)|IPX PATENT PARTNERS|Reg. Nb: 110002789|(CN117358724)|MIAO LIJUAN;BEIJING GAOWO LAW FIRM|Reg. Nb: 11569 (US12595419)|However, generally speaking, household pyrolysis processes and equipment still have shortcomings such as a lack of basic technical theoretical support and insufficient design and development capabilities of equipment, so it is urgent to develop new treatment devices.| (US12595419)|1. A household perishable garbage treatment equipment, comprising a crushing unit, a pyrolysis unit, and a condensation and washing unit; the crushing unit comprises a crushing housing, a cooling water inlet pipe, a crushing device basket, a crushing device, and a cooling water and leachate outlet; a top of the crushing housing is openable, the cooling water inlet pipe is arranged at one side of an upper part of the crushing housing, the crushing device basket is configured for containing perishable organic garbage to be crushed, the crushing device basket is arranged in the crushing housing, the crushing device is arranged in the crushing device basket, and the cooling water and leachate outlet is arranged at a bottom of the crushing housing; the pyrolysis unit comprises a pyrolysis housing, a pyrolysis device basket, solid heat medium, a pyrolysis unit gas outlet, and a heating plate; the pyrolysis device basket is arranged in the pyrolysis housing, the heating plate is arranged at a bottom of the pyrolysis housing, the solid heat medium is arranged inside both the pyrolysis housing and the pyrolysis device basket, the pyrolysis device basket is configured for containing the crushed perishable organic garbage, the pyrolysis unit gas outlet is arranged at one side of an upper part of the pyrolysis housing, and the pyrolysis unit gas outlet is in communication with the condensation and washing unit; the condensation and washing unit comprises a condensation housing, a pyrolysis gas pipeline, a condensation and washing unit gas outlet, a condensation device, a condensate receiving device, a residual exhaust gas discharge pipeline, and an exhaust gas absorption and washing device; the pyrolysis gas pipeline and the condensation and washing unit gas outlet are arranged on an upper part of the condensation housing, an end of the pyrolysis gas pipeline is in communication with the pyrolysis unit gas outlet, another end of the pyrolysis gas pipeline passes through the condensation device and is in communication with the condensate receiving device, an upper part of the condensate receiving device is in communication with an end of the residual exhaust gas discharge pipeline, and another end of the residual exhaust gas discharge pipeline extends to a bottom of the exhaust gas absorption and washing device; and the exhaust gas absorption and washing device is configured for containing condensate; wherein the crushing housing, the pyrolysis housing and the condensation housing are all made of heat-resistant plastic.|9. A use method of a household perishable garbage treatment equipment, comprising the following steps: firstly, crushing perishable organic garbage, that is, placing, by a user, household perishable organic garbage into a crushing device basket, arranging a cover plate on a top of a crushing housing, turning on cooling water, starting a crushing device to crush the perishable organic garbage to a certain extent, wherein cooling water and landfill leachate are discharged into a sewage pipe network through a cooling water and leachate outlet; secondly, performing pyrolysis treatment on the crushed perishable organic garbage, that is, taking out, by the user, the crushing device basket, pouring the crushed perishable organic garbage into a pyrolysis device basket, placing the pyrolysis device basket into a pyrolysis unit, and then filling the pyrolysis unit and the pyrolysis device basket with solid heat medium to fully surround the crushed perishable organic garbage, and then arranging a cover plate on a top of the pyrolysis housing, starting a heating plate for heating, increasing temperature to a certain degree and keeping the temperature for a period of time to achieve full pyrolysis of the perishable organic garbage, wherein gas produced during pyrolysis is discharged into a pyrolysis gas pipeline through a pyrolysis unit gas outlet, and by means of structural features of the pyrolysis device basket, the solid heat medium is capable of being screened and separated, and pyrolysis biochar is capable of being collected regularly; and during pyrolysis, turning on a condensation and washing unit to condense and collect low-boiling pyrolysis liquid in the pyrolysis gas, wherein non-condensable components of the gas are treated by an exhaust gas absorption and washing device and discharged from the device.| (US12595419)|The present disclosure relates to the technical field of environmental engineering, in particular to a household perishable garbage treatment equipment, and a use method thereof.|To achieve the objective above, the present disclosure provides the following technical solution:| (US12595419)|HOUSEHOLD PERISHABLE GARBAGE(100,20)|TREATMENT EQUIPMENT(100,19)|PERISHABLE ORGANIC GARBAGE(53,22)|CRUSHED PERISHABLE ORGANIC GARBAGE(50,12)|PYROLYSIS HOUSING(33,28)|CRUSHING HOUSING(31,22)|CRUSHING PERISHABLE ORGANIC GARBAGE(28,2)|CRUSHED PERISHABLE GARBAGE(27,1)|PYROLYSIS DEVICE BASKET(25,36)|HOUSEHOLD PERISHABLE ORGANIC GARBAGE(25,3)|CONDENSATION(22,38)|PYROLYSIS(22,32)|CRUSHING(22,25)|PYROLYSIS GAS PIPELINE(22,20)|CRUSHING DEVICE BASKET(21,30)|LEACHATE OUTLET(21,12)|PYROLYSIS BIOCHAR(21,2)|CONDENSER HOUSING(18,9)|CONDENSATE(17,18)|EXHAUST GAS ABSORPTION(14,15)|PYROLYTIC BIOCHAR(14,4)|PYROLYSIS UNIT GAS OUTLET(13,21)|CRUSHING BLADE(12,10)|PIPELINE(11,11)|DEVELOPMENT CAPABILITY(11,1)|RESIDUAL EXHAUST GAS(10,12)|PYROLYSIS TREATMENT(10,5)|SEWAGE PIPE NETWORK(10,3)|ENVIRONMENTAL ENGINEERING(10,2)|PERISHABLE GARBAGE TREATMENT MODE(10,2)|HOUSEHOLD PYROLYSIS(10,1)|COOLING WATER(9,19)|HEATING PLATE(9,12)|CRUSHING HOUSING TOP(9,8)|FULL PYROLYSIS(9,4)|LANDFILL LEACHATE(9,4)|YELLOW LOAM(9,2)|PYROLYSIS HOUSING BOTTOM(8,3)|RED LOAM(8,2)|ROCK POWDER(8,2)|BASIC TECHNICAL THEORETICAL SUPPORT(8,1)|INSUFFICIENT DESIGN(8,1)|WASHING UNIT GAS OUTLET(7,9)|PYROLYSIS HOUSING TOP(7,6)|CRUSHING HOUSING BOTTOM(7,3)|STRUCTURAL FEATURE(7,3)|PYROLYSIS GAS(4,7)|COOLING WATER INLET PIPE(4,3)|EXHAUST GAS ABSORPTION BOTTOM(4,3)|GARBAGE SORTING(4,3)|LOW BOILING PYROLYSIS(4,3)|CARBON SEQUESTRATION(4,2)|KAOLIN(4,2)|QUARTZ SAND(4,2)|SOCIAL BENEFIT(4,2)|SORTED GARBAGE(4,2)|SPOT(4,2)|CRUSH PERISHABLE GARBAGE(4,1)|EQUIPMENT STILL(4,1)|HOUSEHOLD PERISHABLE GARBAGE TREATMENT(4,1)|PERISHABLE GARBAGE DECENTRALIZED TREATMENT(4,1)|COVER PLATE(3,11)|TOP MOUNTING HEAD(3,10)|INLET PIPE(3,6)|HEAT RESISTANT PLASTIC(3,5)|STAINLESS STEEL WIRE MESH(3,3)|SODIUM BICARBONATE(3,2)|SODIUM HYDROXIDE(3,2)|SORTED TRANSPORTATION(3,2)|GRADUAL POPULARIZATION(3,1)|HOUSEHOLD COMPOSTING TREATMENT(3,1)|RESIDENT ECOLOGICAL ENVIRONMENT(3,1)|RESIDENT ENTHUSIASM(3,1)|OPEN TOP(2,4)|REMOVEABLE COVER PLATE(2,3)|TREATMENT COST(2,3)|CYLINDRICAL STRUCTURE(2,2)|HYDROCHLORIC ACID(2,2)|INCINERATION TREATMENT(2,2)|LANDFILL TREATMENT(2,2)|ORDINARY SKILL PERSON(2,2)|TREATMENT DECENTRALIZATION(2,2)|TREATMENT SORT(2,2)|ANAEROBIC FERMENTATION(2,1)|BIOCHAR RESOURCE UTILIZATION VALUE(2,1)|CREATIVE EFFORT SHALL FALL(2,1)|CRUSHING BASKET(2,1)|CUBOID MESH BAG(2,1)|EARTHWORM REACTOR(2,1)|GARBAGE EXPLOSION(2,1)|GARBAGE PRODUCTION INTENSITY(2,1)|GARDEN GARBAGE(2,1)|HARMFUL ORGANISM(2,1)|HOUSEHOLD PERISHABLE GARBAGE STRUCTURE(2,1)|HOUSEHOLD TAP(2,1)|INTELLECTUAL PROPERTY ADMINISTRATION(2,1)|KITCHEN WASTE CRUSHING TREATMENT(2,1)|KITCHEN WASTE SORTING(2,1)|PATHOGENIC MICROORGANISM(2,1)|PEOPLE ATTENTION(2,1)|PYROLYSIS DECENTRALIZED TREATMENT EQUIPMENT(2,1)|RESIDENT SORT(2,1)|SEWER PIPE(2,1)|SORTED COLLECTION(2,1)|URBAN LIVING ENVIRONMENT(2,1)|URBAN RESIDENT DAILY LIFE(2,1)|PARTICLE SIZE(1,5)|CRUSHING DEVICE BASKET SURFACE(1,3)|THERMAL INSULATION MATERIAL INSIDE(1,2)|ACCIDENT(1,1)|ANIMAL MANURE(1,1)|CENTRALIZED TREATMENT MODE(1,1)|CENTRALLY TREATED PRODUCT DISTRIBUTION(1,1)|CLIMATE(1,1)|COCKROACH(1,1)|CYLINDRICAL CONDENSER TUBE(1,1)|EVAPORATION TREATMENT EQUIPMENT(1,1)|GARBAGE REMOVAL(1,1)|OBJECTIVE DEMAND(1,1)|ORGANIC GARBAGE COLLECTION(1,1)|PROFESSIONALISM(1,1)|TREATMENT PLANT CENTRALIZATION(1,1)|URBAN ORGANIC WASTE TREATMENT(1,1)||(US20250163330)|HOUSEHOLD PERISHABLE GARBAGE(100,20)|TREATMENT EQUIPMENT(100,19)|GARBAGE TREATMENT EQUIPMENT(100,1)|HOUSEHOLD(100,1)|PERISHABLE GARBAGE TREATMENT EQUIPMENT(100,1)|PERISHABLE ORGANIC GARBAGE(57,22)|CRUSHED PERISHABLE ORGANIC GARBAGE(55,12)|PYROLYSIS HOUSING(34,28)|CRUSHING HOUSING(32,22)|CRUSHING PERISHABLE ORGANIC GARBAGE(31,2)|CRUSHED PERISHABLE GARBAGE(29,1)|HOUSEHOLD PERISHABLE ORGANIC GARBAGE(28,3)|PYROLYSIS DEVICE BASKET(27,36)|CONDENSATION(25,38)|PYROLYSIS(24,32)|CRUSHING(24,25)|PYROLYSIS GAS PIPELINE(24,20)|CRUSHING DEVICE BASKET(23,30)|LEACHATE OUTLET(23,12)|PYROLYSIS BIOCHAR(23,2)|CONDENSATE(18,18)|CONDENSER HOUSING(18,9)|EXHAUST GAS ABSORPTION(15,15)|PYROLYTIC BIOCHAR(15,4)|PYROLYSIS UNIT GAS OUTLET(14,21)|CRUSHING BLADE(13,10)|PIPELINE(12,11)|DEVELOPMENT CAPABILITY(12,1)|RESIDUAL EXHAUST GAS(11,12)|PYROLYSIS TREATMENT(11,5)|SEWAGE PIPE NETWORK(11,3)|ENVIRONMENTAL ENGINEERING(11,2)|PERISHABLE GARBAGE TREATMENT MODE(11,2)|HOUSEHOLD PYROLYSIS(11,1)|HEATING PLATE(10,12)|CRUSHING HOUSING TOP(10,8)|FULL PYROLYSIS(10,4)|LANDFILL LEACHATE(10,4)|YELLOW LOAM(10,2)|COOLING WATER(9,19)|QUARTZ SAND(9,2)|PYROLYSIS HOUSING TOP(8,6)|CRUSHING HOUSING BOTTOM(8,3)|PYROLYSIS HOUSING BOTTOM(8,3)|STRUCTURAL FEATURE(8,3)|RED LOAM(8,2)|ROCK POWDER(8,2)|BASIC TECHNICAL THEORETICAL SUPPORT(8,1)|INSUFFICIENT DESIGN(8,1)|WASHING UNIT GAS OUTLET(7,9)|PYROLYSIS GAS(5,7)|COOLING WATER INLET PIPE(5,3)|CARBON SEQUESTRATION(5,2)|SOCIAL BENEFIT(5,2)|SPOT(5,2)|EQUIPMENT STILL(5,1)|EXHAUST GAS ABSORPTION BOTTOM(4,3)|GARBAGE SORTING(4,3)|LOW BOILING PYROLYSIS(4,3)|KAOLIN(4,2)|SODIUM BICARBONATE(4,2)|SORTED GARBAGE(4,2)|CRUSH PERISHABLE GARBAGE(4,1)|HOUSEHOLD PERISHABLE GARBAGE TREATMENT(4,1)|PERISHABLE GARBAGE DECENTRALIZED TREATMENT(4,1)|COVER PLATE(3,11)|TOP MOUNTING HEAD(3,10)|INLET PIPE(3,6)|STAINLESS STEEL WIRE MESH(3,3)|HYDROCHLORIC ACID(3,2)|INCINERATION TREATMENT(3,2)|SODIUM HYDROXIDE(3,2)|SORTED TRANSPORTATION(3,2)|TREATMENT DECENTRALIZATION(3,2)|ANAEROBIC FERMENTATION(3,1)|CREATIVE EFFORT SHALL FALL(3,1)|CRUSHING BASKET(3,1)|GARBAGE EXPLOSION(3,1)|GARDEN GARBAGE(3,1)|GRADUAL POPULARIZATION(3,1)|HOUSEHOLD COMPOSTING TREATMENT(3,1)|PATHOGENIC MICROORGANISM(3,1)|RESIDENT ECOLOGICAL ENVIRONMENT(3,1)|RESIDENT ENTHUSIASM(3,1)|URBAN LIVING ENVIRONMENT(3,1)|URBAN RESIDENT DAILY LIFE(3,1)|HEAT RESISTANT PLASTIC(2,5)|OPEN TOP(2,4)|CRUSHING DEVICE BASKET SURFACE(2,3)|REMOVEABLE COVER PLATE(2,3)|TREATMENT COST(2,3)|CYLINDRICAL STRUCTURE(2,2)|LANDFILL TREATMENT(2,2)|ORDINARY SKILL PERSON(2,2)|TREATMENT SORT(2,2)|BIOCHAR RESOURCE UTILIZATION VALUE(2,1)|CUBOID MESH BAG(2,1)|EARTHWORM REACTOR(2,1)|GARBAGE PRODUCTION INTENSITY(2,1)|HARMFUL ORGANISM(2,1)|HOUSEHOLD PERISHABLE GARBAGE STRUCTURE(2,1)|HOUSEHOLD TAP(2,1)|INTELLECTUAL PROPERTY ADMINISTRATION(2,1)|KITCHEN WASTE CRUSHING TREATMENT(2,1)|KITCHEN WASTE SORTING(2,1)|PEOPLE ATTENTION(2,1)|PYROLYSIS DECENTRALIZED TREATMENT EQUIPMENT(2,1)|RESIDENT SORT(2,1)|SEWER PIPE(2,1)|SORTED COLLECTION(2,1)|PARTICLE SIZE(1,5)|THERMAL INSULATION MATERIAL INSIDE(1,2)|ACCIDENT(1,1)|ANIMAL MANURE(1,1)|CENTRALIZED TREATMENT MODE(1,1)|CENTRALLY TREATED PRODUCT DISTRIBUTION(1,1)|CLIMATE(1,1)|CYLINDRICAL CONDENSER TUBE(1,1)|EVAPORATION TREATMENT EQUIPMENT(1,1)|GARBAGE REMOVAL(1,1)|OBJECTIVE DEMAND(1,1)|ORGANIC GARBAGE COLLECTION(1,1)|PROFESSIONALISM(1,1)|TREATMENT PLANT CENTRALIZATION(1,1)|URBAN ORGANIC WASTE TREATMENT(1,1)||(JP7719532)|THERMAL DECOMPOSITION(100,35)|CRUSHING(100,21)|COOLING WATER(100,20)|CRUSHING HOUSING(100,18)|CRUSHER BASKET(100,15)|PYROLYZER BASKET(100,15)|CRUSHING DEVICE BASKET(100,12)|SOLID(100,10)|CONDENSATE(100,9)|CRUSHER HOUSING(100,5)|MEDIUM(100,5)|PARTICLE DIAMETER(100,5)|PENETRATING LIQUID OUTLET(100,5)|CONDENSATION WASHING(100,4)|COOLING WATER SUPPLY PIPE(100,4)|HOUSEHOLD(100,4)|INFILTRATION LIQUID OUTLET(100,4)|WATER SUPPLY PIPE(100,4)|OPEN TOP(100,3)|REFUSE DISPOSAL(100,3)|REFUSE TREATMENT(100,3)|SAND(100,3)|TAP WATER(100,3)|TREATING GARBAGE(100,3)|CRUSHING HOUSING TOP(100,2)|CYLINDRICAL STRUCTURE(100,2)|ETHANOL(100,2)|HYDROCHLORIC ACID(100,2)|KAOLIN(100,2)|ORGANIC WASTE(100,2)|QUARTZ SAND(100,2)|ROCK POWDER(100,2)|SODIUM BICARBONATE(100,2)|SODIUM HYDROXIDE(100,2)|RED LOM(100,1)|REFUSE DISPOSAL EQUIPMENT(100,1)|YELLOW LOM(100,1)|MICROBIAL ANAEROBIC FERMENTATION(87,1)|PYROLYTIC HOUSING(69,11)|CONDENSATION CLEANING(66,17)|HOUSEHOLD WASTE DISPOSAL(63,2)|CORRUPT GARBAGE(62,1)|RECEIVING CONDENSATE(57,6)|HOUSEHOLD SEGREGATION TREATMENT(57,1)|SEGREGATED GARBAGE(57,1)|WASTE SORTED COLLECTION(57,1)|FOREST GARBAGE(54,1)|SORTED TRANSPORTATION(50,1)|CONDENSATE WASHING(47,2)|SEGREGATION COLLECTION(47,1)|PYROLYSIS GAS PIPELINE(45,15)|SEGREGATION TRANSPORT(45,1)|SORTED COLLECTION(43,1)|CRUSHING BLADE(41,10)|CONDENSATE WASHING EXHAUST PORT(41,2)|GARBAGE SORTING(41,2)|LAND OCCUPATION AREA(41,2)|AMERICAN FLY(40,1)|INCINERATION TREATMENT(40,1)|CONDENSER HOUSING(39,6)|COMPOSTING TREATMENT(39,1)|HOUSING THERMAL DECOMPOSITION(38,12)|WASTE GENERATION INTENSITY(38,1)|DISCHARGE PIPELINE(37,2)|CENTRALIZED PROCESSING COLLECTION(37,1)|SEGREGATION TREATMENT(37,1)|CENTRALIZED PROCESSING(36,3)|PYROLYTIC UNIT EXHAUST PORT(35,8)|RECYCLING(35,4)|CONDENSATION(33,16)|PYROLYTIC DEVICE BASKET(32,7)|EXHAUST GAS ABSORPTION(31,14)|ORGANIC GARBAGE COLLECTION(31,1)|UNSTABLE TREATMENT(31,1)|RESIDUAL EXHAUST GAS(30,10)|CONDENSATION CLEANING EXHAUST PORT(29,6)|HOUSING CONDENSATE(29,3)|ORGANIC WASTE SORTING(29,1)|FIXED INTERVAL(27,1)|ORGANIC WASTE CORROSION(26,4)|SORTING PROCESSING(26,1)|DEVICE BASKET(25,2)|THERMAL DECOMPOSITION DEVICE BASKET(25,2)|LANDFILL PROCESSING(24,2)|MEDIUM SIZED PREFECTURAL CITY(24,1)|CRUSHER BASKET SURFACE(23,2)|SPOILAGE(23,1)|CLIMATE(22,1)|DIOXIN(22,1)|SMALL PREFECTURAL CITY(22,1)|ENVIRONMENTAL ENGINEERING(21,1)|GARDEN(21,1)|SECONDARY POLLUTANT(21,1)|OPENABLE LID PLATE(20,3)|HEAT EXCHANGER(20,2)|HEATING PLATE(19,11)|UNIT EXHAUST PORT(19,9)|EXHAUST PIPE PATH(18,2)|LARGE LAND OCCUPATION AREA(18,2)|WORM(18,1)|EXHAUST PORT(17,9)|LARGE LAND FOOTPRINT(17,1)|PYROLYSIS(16,7)|THERMAL DECOMPOSITION GAS PIPELINE(16,3)|POPULATION DENSITY(16,1)|PIPELINE(15,7)|ENERGY CONSUMPTION REDUCTION(15,1)|OPERATION EXPERTIZE(15,1)|PYROLYSIS UNIT EXHAUST PORT(14,12)|SOLID HEAT(14,7)|EXHAUST GAS ABSORPTION BOTTOM(14,2)|CORRUPT REFUSE(12,2)|PYROLYZED BIOCHAR(12,2)|CONVERSION EFFICIENCY(12,1)|ENERGY CONSUMPTION(12,1)|PYROLYSIS BIOCHARCOAL PERIODIC COLLECTION(12,1)|GAS PIPELINE(11,3)|CRUSHING BASKET(10,2)|HOUSEHOLD DECAYING REFUSE TREATMENT(10,1)|ORGANIC WASTE(9,12)|TOP MOUNTING HEAD(9,10)|PYROLYSIS HOUSING(9,4)|RECTANGULAR PARALLELEPIPED(9,3)|DOMESTIC DECAYING WASTE(9,1)|OPERATION EXPERTIZE DEGREE(9,1)|RURAL AREA(9,1)|HEAT RESISTANT PLASTIC(8,7)|RESIDENT ECOLOGICAL ENVIRONMENT(8,1)|RESIDENT INITIATIVE(8,1)|DECAYING ORGANIC WASTE(7,3)|CITY LIVING ENVIRONMENT(7,1)|CORROSIVE REFUSE(7,1)|CRUSHED ORGANIC REFUSE(7,1)|GARBAGE CRUSHING TREATMENT(7,1)|GARBAGE EXPLOSION(7,1)|PATHOGENIC MICROORGANISM(7,1)|PYROLYTIC BASKET(7,1)|PYROLYZER BASKET STRUCTURAL FEATURE(7,1)|SORTED GARBAGE(7,1)|SPOILAGE PRONE REFUSE(7,1)|URBAN RESIDENT DAILY LIFE(7,1)|STAINLESS STEEL WIRE MESH(6,3)|HEAT INSULATING MATERIAL(6,2)|INFILTRATION LIQUID DISCHARGE PORT(6,2)|PYROLYSIS APPARATUS BASKET(6,2)|CRUSHER BASKET CENTER(6,1)|CRUSHER BLADE(6,1)|HARMFUL ORGANISM(6,1)|PYROLYZER BASKET MESH DIAMETER(6,1)|REFUSE TREATMENT STRUCTURAL OUTLINE(6,1)|RESIDENT SORT(6,1)|WASTE SPOILATION(6,1)|SEWERAGE(5,2)|CENTRALIZED PROCESSING PLANT(5,1)|CLEANING UP(5,1)|PROCESSING DEPARTMENT COLLECT(5,1)|SOIL PURIFICATION(5,1)|SPOILAGE PRONE WASTE(5,1)|STILL ROOM(5,1)|TRANSPORT SYSTEM(5,1)|WASTE INFILTRATION LIQUID(5,1)|PYROLYSIS GAS(4,4)|THERMAL DECOMPOSITION TREATMENT(4,4)|CARBON SEGREGATION(4,1)|CONDENSER TUBE(4,1)|DEVELOPMENT CAPABILITY(4,1)|EVAPORATION TREATMENT EQUIPMENT(4,1)|HOME COMPOSTING TREATMENT(4,1)|HOME TAP WATER FAUCET(4,1)|HOUSING CRUSHED ORGANIC(4,1)|INCINERATION PROCESSING(4,1)|LIQUID PERMEATION(4,1)|MUNICIPAL ORGANIC WASTE(4,1)|PERMEATING LIQUID DISCHARGE PORT(4,1)||(JP2025084647)|HOUSEHOLD PERISHABLE GARBAGE(100,4)|TREATMENT EQUIPMENT(100,4)|HOUSEHOLD PUTREFYING REFUSE(60,1)|PERISHABLE ORGANIC REFUSE(54,2)|HOUSEHOLD PUTREFYING REFUSE TREATMENT(54,1)|CRUSHING HOUSING(52,22)|CRUSHER BASKET(47,16)|MICROBIAL ANAEROBIC FERMENTATION(45,1)|CONDENSATION CLEANING(43,22)|HUMULUS ORYZAE(42,2)|HOUSEHOLD PERISHABLE(38,1)|HOUSEHOLD WASTE DISPOSAL(37,2)|CRUSHED PERISHABLE GARBAGE(37,1)|PYROLYZER BASKET(35,9)|HOUSEHOLD PERISHABLE REFUSE(35,1)|PYROLYTIC APPARATUS BASKET(34,2)|RECEIVING CONDENSATE(33,11)|CRUSHING(32,16)|PERISHABLE ORGANIC WASTE(32,12)|PYROLYZING APPARATUS BASKET(32,8)|WASTE SEGREGATION COLLECTION(32,1)|PYROLYSIS HOUSING(31,4)|PYROLYZED BIOCHAR(30,2)|PYROLYZING HOUSING(29,4)|DECOMPOSED ORGANIC REFUSE(28,2)|PERMEATING LIQUID DISCHARGE PORT(27,7)|GARDEN GARBAGE(27,1)|HOME SPOILED GARBAGE TREATMENT(27,1)|PYROLYTIC HOUSING(26,1)|YELLOW LOME(26,1)|HOME SPOILED GARBAGE(25,1)|PYROLYSIS EXHAUST PORT(25,1)|PYROLYTIC BIOCHAR(25,1)|SEGREGATION COLLECTION(25,1)|BASKET STRUCTURAL FEATURE(24,1)|THERMAL DECOMPOSITION(23,84)|CRUSHING DEVICE BASKET(23,10)|RED LOME(23,1)|SEGREGATION TRANSPORT(23,1)|CONDENSATION CLEANING EXHAUST PORT(22,9)|CONDENSER HOUSING(22,9)|RECYCLING(21,3)|CENTRALIZED PROCESSING(21,2)|CONDENSATION WASHING(21,2)|TREATING GARBAGE(21,1)|THERMAL DECOMPOSITION GAS PIPELINE(20,16)|PYROLYTIC UNIT EXHAUST PORT(20,2)|EXHAUST PIPELINE(19,3)|QUARTZ SAND(19,2)|CENTRALIZED PROCESSING COLLECTION(19,1)|GAS PIPELINE(18,16)|CONDENSATION(18,15)|ROCK POWDER(18,2)|ABLE GARBAGE TREATMENT(18,1)|PYROLYTIC DEVICE BASKET(18,1)|CRUSHING BLADE(17,8)|CONDENSATE(17,3)|DOMESTIC DECAY(17,1)|RESOURCE UTILIZATION(17,1)|COOLING WATER(16,21)|EXHAUST GAS ABSORPTION(16,14)|PYROLYSIS(16,8)|CRUSHING HOUSING TOP(16,5)|PIPELINE(16,3)|GARBAGE SEPARATION(16,2)|BIOTREATMENT(16,1)|HOUSEHOLD WASTE TREATMENT(16,1)|TECHNICAL THEORY(16,1)|PYROLYTIC GAS(15,3)|LANDFILL TREATMENT(15,2)|PERISHABLE GARBAGE TREATMENT MODE(15,2)|PYROLYTIC LIQUID(15,2)|PYROLYZER(15,2)|DEVELOPMENT CAPABILITY(15,1)|SEGREGATION PROCESSING(15,1)|SEPARATED GARBAGE(15,1)|TRANSPORTATION(15,1)|RESIDUAL EXHAUST GAS(14,12)|LID PLATE(14,4)|ORGANIC REFUSE(14,4)|SEWAGE PIPE NETWORK(14,3)|HOUSEHOLD PYROLYSIS(14,1)|HEATING PLATE(13,11)|PYROLYSIS GAS PIPELINE(13,4)|CONDENSATE(13,2)|COMPOSTING(13,1)|UNSTABLE PROCESSING(13,1)|CRUSHER BASKET SURFACE(12,2)|PYROLYZING UNIT EXHAUST PORT(12,2)|LAND AREA OCCUPATION(12,1)|EXHAUST PORT(11,12)|PYROLYSIS(11,3)|INCINERATION(11,2)|STRUCTURAL FEATURE(11,2)|CLIMATE(11,1)|DIOXIN(11,1)|INSUFFICIENT DESIGN(11,1)|SODIUM HYDROGENCARBONATE(10,2)|FOCUS(10,1)|OPERATION SPECIALIZATION(10,1)|PROCESSING EQUIPMENT(10,1)|SECONDARY POLLUTANT(10,1)|TREATED GAS COMPONENT(10,1)|WASTE TREATMENT(10,1)|HOUSING THERMAL DECOMPOSITION(9,16)|CRUSHER(9,8)|HOUSEHOLD(9,3)|PARTICLE DIAMETER(9,3)|FIXED INTERVAL(9,2)|KAOLIN(9,2)|ORGANIC WASTE(9,2)|UNIT EXHAUST PORT(8,17)|ORGANIC WASTE(8,7)|CARBON SEQUESTRATION(8,1)|COOLING WATER SUPPLY PIPE(7,4)|WATER SUPPLY PIPE(7,4)|GAS COMPONENT(7,3)|SAND(7,3)|ENVIRONMENTAL ENGINEERING(7,2)|EXHAUST GAS ABSORPTION BOTTOM(7,2)|OPENABLE COVER PLATE(7,2)|SODIUM HYDROXIDE(7,2)|SPOT(7,2)|ENERGY CONSUMPTION REDUCTION(7,1)|LARGE INFLUENCE(7,1)|DEVICE BASKET(6,9)|THERMAL DECOMPOSITION DEVICE BASKET(6,9)|BOILING POINT PYROLYTIC LIQUID(6,2)|HYDROCHLORIC ACID(6,2)|SOCIAL BENEFIT(6,2)|CONVERSION EFFICIENCY(6,1)|CRUSHED PERISHABLE REFUSE(6,1)|ENERGY CONSUMPTION(6,1)|PYROLYSIS HOUSING TOP PLATE(6,1)|CYLINDRICAL STRUCTURE(5,2)|PYROLYSIS BASKET(5,2)|DISPERSAL TREAT PERISHABLE GARBAGE(5,1)|LARGE LAND OCCUPIED AREA(5,1)|PYROLYZED BIOCHARCOAL(5,1)|RURAL AREA(5,1)|TEMPERATURE RISE(5,1)|TOP MOUNTING HEAD(4,10)|HEAT RESISTANT PLASTIC(4,6)|OSMOTIC LIQUID DISCHARGE PORT(4,5)|CRUSHER HOUSING(4,3)|TAP WATER(4,3)|CRUSHER BLADE(4,2)|PERISHABLE GARBAGE DISPOSAL(4,1)|PUTREFYING REFUSE DISPOSAL(4,1)|RESIDENT ECOLOGICAL ENVIRONMENT(4,1)|RESIDENT GARBAGE(4,1)|RESIDENT WILLINGNESS(4,1)|STAINLESS STEEL WIRE MESH(3,3)|CONDENSER RECEIVER(3,2)|DISCHARGE CONDUIT(3,2)|DISCHARGE PIPELINE(3,2)|RECTANGULAR PARALLELEPIPED(3,2)|CRUSHED PERISHABLE ORGANIC WASTE(3,1)|CRUSHER BASKET CENTER(3,1)|CRUSHING BASKET(3,1)|GARBAGE CRUSHING TREATMENT(3,1)|GARBAGE EXPLOSION(3,1)|GARDENING GARBAGE(3,1)|HOUSEHOLD REFUSE DISPOSAL(3,1)|MIZU REACTOR(3,1)|PATHOGENIC MICROORGANISM(3,1)|PYROLYZER BASKET STRUCTURAL FEATURE(3,1)|REFUSE OSMOTIC LIQUID(3,1)|SORTED ORGANIC WASTE SORTING(3,1)|TREATMENT COST(3,1)|TREATMENT DEPARTMENT COLLECT(3,1)|URBAN LIVING ENVIRONMENT(3,1)|URBAN RESIDENT DAILY LIFE(3,1)|BOILING POINT(2,3)|PYROLYSIS DEVICE BASKET(2,2)|SEWER(2,2)|CENTRALIZED TREATMENT MODE(2,1)|CONDENSER PIPE(2,1)|CORE IDEA(2,1)|EVAPORATION TREATMENT EQUIPMENT(2,1)|FEEDWATER PIPE(2,1)|HOME COMPOSTING TREATMENT(2,1)|HOME TAP WATER FAUCET(2,1)|LARGE AREA(2,1)|LARGE LAND AREA(2,1)|MUNICIPAL ORGANIC WASTE(2,1)|OPENABLE LID PLATE(2,1)|PYROLYZED GAS(2,1)|PYROLYZING(2,1)|RED ROME(2,1)|REMOVAL HIGH COST(2,1)|THERMAL DECOMPOSITION BIOCHARCOAL(2,1)|WASTE GENERATION INTENSITY(2,1)|YELLOW ROME(2,1)||(CN117358724)|HOUSEHOLD PERISHABLE GARBAGE TREATMENT(100,4)|CRUSHING BLADE(37,2)|PERISHABLE GARBAGE DISPOSAL(37,1)|PERISHABLE GARBAGE TREATMENT MODE(30,1)|ECOLOGICAL BENEFIT(29,1)|ECONOMIC BENEFIT(26,1)|PYROLYSIS HOUSING(22,1)|RED LOAM(22,1)|YELLOW LOAM(21,2)|CRUSHING DEVICE BASKET(20,3)|QUARTZ SAND(20,2)|STONE POWDER(18,2)|TREATMENT EQUIPMENT(15,1)|DOMESTIC(14,1)|SOCIAL BENEFIT(14,1)|CARBON SEQUESTRATION(13,1)|PYROLYSIS DEVICE BASKET(12,9)|PYROLYSIS SHELL(12,5)|CRUSHING SHELL(11,4)|TOP MOUNTING HEAD(11,3)|COLLECTION TREATMENT COST(11,1)|MICROORGANISM ANAEROBIC FERMENTATION(11,1)|KAOLIN(9,2)|CRUSHED PERISHABLE ORGANIC GARBAGE(9,1)|CONDENSING WASHING(7,2)|CYLINDRICAL STRUCTURE(7,1)|COMPOSTING TREATMENT(6,2)|INCINERATION TREATMENT(6,2)|OPEN TOP(6,2)|CRUSHING BASKET(6,1)|PYROLYSIS BASKET(6,1)|CONDENSATE(5,4)|LANDFILL TREATMENT(5,2)|PYROLYSIS GAS PIPELINE(5,2)|PYROLYSIS TREATMENT(5,2)|CONDENSING SHELL(5,1)|CONDENSING WASHING(5,1)|DEFECT(4,3)|BROKEN PERISHABLE(4,1)|CONDENSATION SHELL(4,1)|RESOURCE WASTE(4,1)|STAINLESS STEEL WIRE MESH(4,1)|PARTICLE SIZE(3,3)|GRAIN DIAMETER(3,2)|CENTRALIZED TREATMENT MODE(3,1)|CENTRALIZED TREATMENT PLANT(3,1)|FULL PYROLYSIS(3,1)|HERMETIA ILLUCENS(3,1)|INSULATING MATERIAL(3,1)|OUTER WALL(3,1)|RESIDUAL TAIL GAS(3,1)|TAIL GAS DISCHARGE PIPELINE(3,1)| (US12595419)|What is claimed is:|1. A household perishable garbage treatment equipment, comprising a crushing unit, a pyrolysis unit, and a condensation and washing unit;| the crushing unit comprises a crushing housing, a cooling water inlet pipe, a crushing device basket, a crushing device, and a cooling water and leachate outlet; a top of the crushing housing is openable, the cooling water inlet pipe is arranged at one side of an upper part of the crushing housing, the crushing device basket is configured for containing perishable organic garbage to be crushed, the crushing device basket is arranged in the crushing housing, the crushing device is arranged in the crushing device basket, and the cooling water and leachate outlet is arranged at a bottom of the crushing housing;| the pyrolysis unit comprises a pyrolysis housing, a pyrolysis device basket, solid heat medium, a pyrolysis unit gas outlet, and a heating plate; the pyrolysis device basket is arranged in the pyrolysis housing, the heating plate is arranged at a bottom of the pyrolysis housing, the solid heat medium is arranged inside both the pyrolysis housing and the pyrolysis device basket, the pyrolysis device basket is configured for containing the crushed perishable organic garbage, the pyrolysis unit gas outlet is arranged at one side of an upper part of the pyrolysis housing, and the pyrolysis unit gas outlet is in communication with the condensation and washing unit;| the condensation and washing unit comprises a condensation housing, a pyrolysis gas pipeline, a condensation and washing unit gas outlet, a condensation device, a condensate receiving device, a residual exhaust gas discharge pipeline, and an exhaust gas absorption and washing device; the pyrolysis gas pipeline and the condensation and washing unit gas outlet are arranged on an upper part of the condensation housing, an end of the pyrolysis gas pipeline is in communication with the pyrolysis unit gas outlet, another end of the pyrolysis gas pipeline passes through the condensation device and is in communication with the condensate receiving device, an upper part of the condensate receiving device is in communication with an end of the residual exhaust gas discharge pipeline, and another end of the residual exhaust gas discharge pipeline extends to a bottom of the exhaust gas absorption and washing device; and the exhaust gas absorption and washing device is configured for containing condensate;| wherein the crushing housing, the pyrolysis housing and the condensation housing are all made of heat-resistant plastic.|2. The household perishable garbage treatment equipment according to claim 1, wherein removable cover plates are arranged on the top of the crushing housing and a top of the pyrolysis housing, respectively.|3. The household perishable garbage treatment equipment according to claim 1, wherein the crushing device comprises a crushing blade, a blade mounting rod, and a top mounting head; the crushing blade is arranged on an outer wall of the blade mounting rod, the top mounting head is arranged on a top of the blade mounting rod, and the top mounting head is configured to be connected to a driving device.|4. The household perishable garbage treatment equipment according to claim 1, wherein the crushing device basket is of a cylindrical structure with an open top, and a plurality of holes are evenly distributed on a surface of the crushing device basket at intervals.|5. The household perishable garbage treatment equipment according to claim 1, wherein the pyrolysis device basket is of a mesh bag shaped structure with an open top, and the pyrolysis device basket is made of stainless-steel wire mesh.|6. The household perishable garbage treatment equipment according to claim 1, wherein the solid heat medium is one or more of sand, kaolin, quartz sand, stone powder, yellow loam and red loam with a particle size less than 5 mm.|7. The household perishable garbage treatment equipment according to claim 1, wherein the pyrolysis housing is lined with thermal insulation material inside.|8. The household perishable garbage treatment equipment according to claim 1, wherein the condensate is tap water, sodium hydroxide, dilute hydrochloric acid, sodium bicarbonate, or ethanol.|9. A use method of a household perishable garbage treatment equipment, comprising the following steps:| firstly, crushing perishable organic garbage, that is, placing, by a user, household perishable organic garbage into a crushing device basket, arranging a cover plate on a top of a crushing housing, turning on cooling water, starting a crushing device to crush the perishable organic garbage to a certain extent, wherein cooling water and landfill leachate are discharged into a sewage pipe network through a cooling water and leachate outlet;| secondly, performing pyrolysis treatment on the crushed perishable organic garbage, that is, taking out, by the user, the crushing device basket, pouring the crushed perishable organic garbage into a pyrolysis device basket, placing the pyrolysis device basket into a pyrolysis unit, and then filling the pyrolysis unit and the pyrolysis device basket with solid heat medium to fully surround the crushed perishable organic garbage, and then arranging a cover plate on a top of the pyrolysis housing, starting a heating plate for heating, increasing temperature to a certain degree and keeping the temperature for a period of time to achieve full pyrolysis of the perishable organic garbage, wherein gas produced during pyrolysis is discharged into a pyrolysis gas pipeline through a pyrolysis unit gas outlet, and by means of structural features of the pyrolysis device basket, the solid heat medium is capable of being screened and separated, and pyrolysis biochar is capable of being collected regularly; and| during pyrolysis, turning on a condensation and washing unit to condense and collect low-boiling pyrolysis liquid in the pyrolysis gas, wherein non-condensable components of the gas are treated by an exhaust gas absorption and washing device and discharged from the device. (US12595419)|CROSS-REFERENCE TO RELATED APPLICATION|[0001] This patent application claims the benefit and priority of Chinese Patent Application No. 202311567112.0 filed with the China National Intellectual Property Administration on Nov. 22, 2023, the disclosure of which is incorporated by reference herein in its entirety as part of the present application.|(US12595419)|TECHNICAL FIELD|[0002] The present disclosure relates to the technical field of environmental engineering, in particular to a household perishable garbage treatment equipment, and a use method thereof.|BACKGROUND|[0003] Household perishable garbage usually refers to organic solid waste produced in the daily life of urban residents, mainly including kitchen waste, garden waste, human and animal manure and so on.|[0004] Perishable garbage has the following hazards: harmful gases such as ammonia and sulfide released by the perishable garbage piled up outdoors will pollute the atmosphere and urban living environment; high-concentration leachate produced in the process of piling and spoilage will seriously pollute the water body; it is easy to breed pathogenic microorganisms, mosquitoes, flies, cockroaches, mice, and other harmful organisms, affecting the health of residents; a lot of land is occupied; and accidents such as garbage explosions may be caused. Therefore, serious harm will be caused to the lift and ecological environment of residents if urban organic waste cannot be effectively treated, and thus the treatment of urban organic waste must be paid attention to by all parties.|[0005] The traditional main treatment mode for perishable garbage mainly adopts a centralized treatment mode, that is, household garbage in a city is collected uniformly and transported to a centralized treatment plant for treatment. Common methods include composting treatment, incineration treatment, pyrolysis treatment, landfill treatment and biological treatment, etc., but the existing centralized treatment methods need to be further improved. For example, composting treatment has the disadvantages of relatively low treatment efficiency, unstable treatment process caused by different components of waste, and large floor area. Incineration treatment has the disadvantages of the risk of producing secondary pollutants such as dioxins, and waste of resources. Pyrolysis treatment has the disadvantages of strong professionalism in operation, and limited pathways for resource utilization of existing products. Landfill treatment has the disadvantages of large floor area and high removal cost. The use of biological treatment processes such as black soldier flies, earthworms and anaerobic fermentation by microorganisms has the disadvantages of relatively low conversion efficiency, great influence by climate and other environments, and large floor area.|[0006] On the other hand, with the gradual popularization and implementation of garbage sorting in cities and rural areas, requirements for sorted collection, sorted transportation and sorted treatment of household perishable garbage such as sorted kitchen waste and garden garbage have been put forward, while an independent organic garbage collection and transportation system is huge and complicated, with high cost and many problems. These problems are particularly serious in small and medium-sized counties and cities with low population density and low garbage production intensity, and the current separate treatment technology for sorted organic garbage still needs to be improved. As a result, residents sort their garbage at the source, but the sorted garbage is mixed together again by garbage removal and treatment units for removal or treatment, which greatly dampens the enthusiasm of residents to implement garbage sorting and delays the popularization and implementation of garbage sorting.|[0007] The existence of the above problems puts forward an objective demand for decentralized treatment of perishable garbage at the source, that is, the garbage is sorted at the source with families as the unit and effectively treated, which not only can solve the problems of sorted transportation and sorted treatment faced by the sorted and collected garbage at present, but also can achieve the resource utilization of products at the source, thus reducing energy consumption in the processes of centralized treatment, removal and collection, resource utilization and distribution of centrally treated products and the like. While reducing treatment cost, significant carbon emission reduction effect and obvious social and environmental benefits are achieved.|[0008] At present, the commonly used decentralized treatment technologies for organic waste in China and at abroad include kitchen waste crushing treatment technology, household composting treatment technology, earthworm reactor, water evaporation treatment equipment, small-scale pyrolysis equipment, etc. The small-scale pyrolysis decentralized treatment equipment for organic waste has attracted attention of people due to its advantages of high treatment efficiency, relatively stable process and high value of biochar resource utilization from pyrolysis products. However, generally speaking, household pyrolysis processes and equipment still have shortcomings such as a lack of basic technical theoretical support and insufficient design and development capabilities of equipment, so it is urgent to develop new treatment devices.|SUMMARY|[0009] For addressing the disadvantages in the existing household perishable garbage treatment, a novel and efficient treatment equipment and a use method thereof is proposed in the present disclosure.|[0010] To achieve the objective above, the present disclosure provides the following technical solution:|[0011] A household perishable garbage treatment equipment, including a crushing unit, a pyrolysis unit, and a condensation and washing unit.|[0012] The crushing unit includes a crushing housing, a cooling water inlet pipe, a crushing device basket, a crushing device, and a cooling water and leachate outlet. A top of the crushing housing is openable, the cooling water inlet pipe is arranged at one side of an upper part of the crushing housing, the crushing device basket is configured for containing perishable organic garbage to be crushed, the crushing device basket is arranged in the crushing housing, the crushing device is arranged in the crushing device basket, and the cooling water and leachate outlet is arranged at a bottom of the crushing housing.|[0013] The pyrolysis unit includes a pyrolysis housing, a pyrolysis device basket, solid heat medium, a pyrolysis unit gas outlet, and a heating plate. The pyrolysis device basket is arranged in the pyrolysis housing, the heating plate is arranged at a bottom of the pyrolysis housing, the solid heat medium is arranged inside both the pyrolysis housing and the pyrolysis device basket, the pyrolysis device basket is configured for containing the crushed perishable organic garbage, the pyrolysis unit gas outlet is arranged at one side of an upper part of the pyrolysis housing, and the pyrolysis unit gas outlet is in communication with the condensation and washing unit.|[0014] The condensation and washing unit includes a condensation housing, a pyrolysis gas pipeline, a condensation and washing unit gas outlet, a condensation device, a condensate receiving device, a residual exhaust gas discharge pipeline, and an exhaust gas absorption and washing device. The pyrolysis gas pipeline and the condensation and washing unit gas outlet are arranged on an upper part of the condensation housing, an end of the pyrolysis gas pipeline is in communication with the pyrolysis unit gas outlet, another end of the pyrolysis gas pipeline passes through the condensation device and is in communication with the condensate receiving device, an upper part of the condensate receiving device is in communication with an end of the residual exhaust gas discharge pipeline, and another end of the residual exhaust gas discharge pipeline extends to a bottom of the exhaust gas absorption and washing device; and the exhaust gas absorption and washing device is configured for containing condensate.|[0015] Optionally, the crushing housing, the pyrolysis housing and the condensation housing are all made of heat-resistant plastic.|[0016] Optionally, removable cover plates are arranged on the top of the crushing housing and a top of the pyrolysis housing, respectively.|[0017] Optionally, the crushing device includes a crushing blade, a blade mounting rod, and a top mounting head. The crushing blade is arranged on an outer wall of the blade mounting rod, the top mounting head is arranged on a top of the blade mounting rod, and the top mounting head is configured to be connected to a driving device.|[0018] Optionally, the crushing device basket is of a cylindrical structure with an open top, and multiple holes are evenly distributed on a surface of the crushing device basket at intervals.|[0019] Optionally, the pyrolysis device basket is of a mesh bag shaped structure with an open top, and the pyrolysis device basket is made of stainless-steel wire mesh.|[0020] Optionally, the solid heat medium is one or more of sand, kaolin, quartz sand, stone powder, yellow loam and red loam with a particle size less than 5 mm.|[0021] Optionally, the pyrolysis housing is lined with thermal insulation material inside.|[0022] Optionally, the condensate is tap water, sodium hydroxide, dilute hydrochloric acid, sodium bicarbonate, or ethanol.|[0023] A use method of a household perishable garbage treatment equipment is further proposed in the present disclosure. The method includes the following steps: firstly, crushing perishable organic garbage, that is, placing, by a user, household perishable organic garbage into a crushing device basket, arranging a cover plate on a top of a crushing housing, turning on cooling water, starting a crushing device to crush the perishable organic garbage to a certain extent, wherein cooling water and landfill leachate are discharged into a sewage pipe network through a cooling water and leachate outlet; secondly, performing pyrolysis treatment on the crushed perishable organic garbage, that is, taking out, by the user, the crushing device basket, pouring the crushed perishable organic garbage into a pyrolysis device basket, placing the pyrolysis device basket into a pyrolysis unit, filling the pyrolysis unit and the pyrolysis device basket with solid heat medium to fully surround the crushed perishable organic garbage, and then arranging a cover plate on a top of the pyrolysis housing, starting a heating plate for heating, increasing temperature to a certain degree and keeping the temperature for a period of time to achieve full pyrolysis of the perishable organic garbage, wherein gas produced during pyrolysis is exhausted into a pyrolysis gas pipeline through a pyrolysis unit gas outlet, and by means of structural features of the pyrolysis device basket, the solid heat medium is capable of being screened and separated, and pyrolysis biochar is capable of being collected regularly; and during pyrolysis, turning on a condensation and washing unit to condense and collect low-boiling pyrolysis liquid in the pyrolysis gas, wherein non-condensable components of the gas are treated by an exhaust gas absorption and washing device and discharged from the device.|[0024] Compared with the prior art, the present disclosure obtains the following beneficial technical effects:|[0025] In the present disclosure, the household perishable garbage treatment equipment and the use method thereof can effectively treat perishable garbage on the spot, reduce the collection and treatment cost required by traditional perishable garbage treatment modes, achieve carbon sequestration and resource utilization of products, and have significant economic, ecological and social benefits.|(US12595419)|BRIEF DESCRIPTION OF THE DRAWINGS|[0026] To describe the technical solutions in the embodiments of the present disclosure or in the prior art more clearly, the following briefly introduces the accompanying drawings required for describing the embodiments. Apparently, the accompanying drawings in the following description show merely some embodiments of the present disclosure, and those of ordinary skill in the art may still obtain other drawings from these accompanying drawings without creative efforts.|[0027] FIG. 1 is a schematic diagram of structure of a household perishable garbage treatment equipment according to an embodiment of the present disclosure.|(US12595419)|DETAILED DESCRIPTION|[0028] In the drawings: 1—crushing unit; 2—pyrolysis unit; 3—condensation and washing unit; 1-1—cooling water inlet pipe; 1-2—crushing device basket; 1-3—crushing device; 1-4—perishable organic garbage to be crushed; 1-5—cooling water and leachate outlet; 2-1—pyrolysis device basket; 2-2—solid heat medium; 2-3—pyrolysis unit gas outlet; 2-4—heating plate; 2-5—pyrolytic biochar; 3-1—pyrolysis gas pipeline; 3-2—condensation and washing unit gas outlet; 3-3—condensation device; 3-4—condensate receiving device; 3-5—residual exhaust gas discharge pipeline; 3-6—exhaust gas absorption and washing device.|DETAILED DESCRIPTION OF THE EMBODIMENTS|[0029] The following clearly and completely describes the technical solutions in the embodiments of the present disclosure with reference to the accompanying drawings in the embodiments of the present disclosure. Apparently, the described embodiments are merely a part rather than all of the embodiments of the present disclosure. All other embodiments obtained by a person of ordinary skill in the art based on the embodiments of the present disclosure without creative efforts shall fall within the protection scope of the present disclosure.|Embodiment 1|[0030] As shown in FIG. 1, the present embodiment provides a household perishable garbage treatment equipment, including a crushing unit 1, a pyrolysis unit 2, and a condensation and washing unit 3.|[0031] The crushing unit 1 includes a crushing housing, a cooling water inlet pipe 1-1, a crushing device basket 1-2, a crushing device 1-3, and a cooling water and leachate outlet 1-5. A top of the crushing housing is openable, the cooling water inlet pipe 1-1 is arranged at one side of an upper part of the crushing housing, the crushing device basket 1-2 is configured for containing perishable organic garbage to be crushed 1-4, the crushing device basket 1-2 is arranged in the crushing housing, the crushing device 1-3 is arranged in the crushing device basket 1-2, and the cooling water and leachate outlet 1-5 is arranged at a bottom of the crushing housing.|[0032] The pyrolysis unit 2 includes a pyrolysis housing, a pyrolysis device basket 2-1, solid heat medium 2-2, a pyrolysis unit gas outlet 2-3, and a heating plate 2-4. The pyrolysis device basket 2-1 is arranged in the pyrolysis housing, the heating plate 2-4 is arranged at a bottom of the pyrolysis housing, the solid heat medium 2-2 is arranged inside both the pyrolysis housing and the pyrolysis device basket 2-1, the pyrolysis device basket 2-1 is configured for containing the crushed perishable organic garbage, the pyrolysis unit gas outlet 2-3 is arranged at one side of an upper part of the pyrolysis housing, and the pyrolysis unit gas outlet 2-3 is in communication with the condensation and washing unit 3.|[0033] The condensation and washing unit 3 includes a condensation housing, a pyrolysis gas pipeline 3-1, a condensation and washing unit gas outlet 3-2, a condensation device 3-3, a condensate receiving device 3-4, a residual exhaust gas discharge pipeline 3-5, and an exhaust gas absorption and washing device 3-6. The pyrolysis gas pipeline 3-1 and the condensation and washing unit gas outlet 3-2 are arranged on an upper part of the condensation housing, an end of the pyrolysis gas pipeline 3-1 is in communication with the pyrolysis unit gas outlet 3-2, another end of the pyrolysis gas pipeline 3-1 passes through the condensation device 3-3 and is in communication with the condensate receiving device 3-4, an upper part of the condensate receiving device 3-4 is in communication with an end of the residual exhaust gas discharge pipeline 3-5, and another end of the residual exhaust gas discharge pipeline 3-5 extends to a bottom of the exhaust gas absorption and washing device 3-6; and the exhaust gas absorption and washing device 3-6 is configured for containing condensate.|[0034] In this specific embodiment, the crushing housing is made of heat-resistant plastic, which is of a cuboid structure with a length, width and height of 25 cm x 30 cm x 30 cm. When a cover plate is removed, the crushing device 1-3 can be installed, which includes a crushing blade, a blade mounting rod, and a top mounting head. The crushing blade is arranged on an outer wall of the blade mounting rod, and the top mounting head is arranged on a top of the blade mounting rod, and the top mounting head is configured to be connected to a driving device. The crushing blade is a propeller-shaped stainless-steel blade with a total length of 10 cm at the bottom. The crushing blade mounting rod is a stainless-steel rod with a diameter of 10 mm and a height of 15 cm. The top mounting head is connected to a power supply and can rotate the crushing blade to cut and crush perishable garbage. The crushing device basket 1-2 has a diameter of 20 cm and a height of 17 cm, and is made of stainless steel. Circular holes with a diameter of 0.5 cm are evenly distributed on a surface of the crushing device basket at intervals of 3 cm. The blade of the crushing device 1-3 is installed and fixed at the center of the crushing device basket 1-2, and thus the crushing device basket 1-2 can be hung in the crushing unit 1 by a hook.|[0035] After the crushing device basket and crushing device 1-3 are installed, the perishable garbage can be placed in the basket, then the cover plate is arranged, cooling water is turned on, and the crushing device 1-3 is started for crushing. The cooling water inlet pipe 1-1 has a diameter of 2 cm and is connected to a household tap, and a water outlet of the cooling water inlet pipe 1-1 is located above the crushing device basket 1-2. The cooling water is sprayed in a direction tangential to the rotation of the blade, thus playing a role in cooling and cleaning. During crushing, the cooling water and landfill leachate are discharged into a sewer through the cooling water and leachate outlet 1-5, and the cooling water and leachate outlet 1-5 has a diameter of 2 cm, a lower part of which is directly connected to a sewer pipe with a plastic hose.|[0036] The pyrolysis housing is made of the heat-resistant plastic. A removable cover plate is arranged on a top of the pyrolysis housing. The pyrolysis housing is of a cuboid structure with a length, width and height of 10 cm x 30 cm x 30 cm. The pyrolysis housing is lined with thermal insulation cotton inside. The cover plate can be removed from an upper part of the pyrolysis unit 2 for placing or taking out the pyrolysis device basket 2-1. The pyrolysis device basket 2-1 is of a cuboid mesh bag shaped structure with a hollow upper part and closed at periphery and bottom, and with a length, width and height of 9 cm x 28 cm x 28 cm. The mesh bag is made of stainless-steel wire mesh with a hole diameter of 5 mm. The solid heat medium 2-2 is placed in the pyrolysis unit 2, and the solid heat medium 2-2 is sand with a particle size less than 2 mm.|[0037] After the perishable garbage is crushed in the crushing unit 1, the crushing device basket 1-2 can be taken out, the crushed perishable garbage in the crushing basket is poured into the pyrolysis device basket. Then, the pyrolysis device basket 2-1 is fixed into the pyrolysis unit 2 by a hook, the periphery of the pyrolysis device basket 2-1 is filled with the solid heat medium 2-2, such that the periphery of the crushed perishable organic garbage can be fully surround by the solid heat medium 2-2. After that, the cover plate is arranged on the pyrolysis unit 2, the heating plate 2-4 is started, and after the temperature is increased to a certain degree and kept for a period of time, full pyrolysis of perishable organic garbage can be achieved. The heating plate 2-4 is installed at a bottom of the pyrolysis unit 2, with a length, width and thickness of 9 cm x 28 cm x 1 cm, and is made of a stainless-steel plate containing heat wires. During pyrolysis, when the cover plate is arranged at the upper part of the pyrolysis unit 2, the pyrolysis gas can only be discharged from the pyrolysis unit 2 through the pyrolysis unit gas outlet 2-3. The pyrolysis unit gas outlet 2-3 is a heat-resistant plastic circular tube with a diameter of 3 cm, which has a length of 2 cm inside the pyrolysis unit 2 and a mesh cover wrapped outside. The pyrolysis unit gas outlet 2-3 is connected to the pyrolysis gas pipeline 3-1 in the condensation and washing unit 3, and the produced gas is discharged into the pyrolysis gas pipeline 3-1 from the pyrolysis unit gas outlet 2-3.|[0038] After pyrolysis is finished, the pyrolysis device basket 2-1 is taken out from the pyrolysis unit 2. Under the action of gravity, the solid heat medium 2-2 with a particle size less than the mesh diameter of the pyrolysis device basket 2-1 falls from the basket, and the pyrolytic biochar 2-5 with a particle size greater than 5 mm after pyrolysis is intercepted into the basket and then taken out of the device.|[0039] The condensation housing is made of heat-resistant plastic, the condensation and washing unit 3 is of a cuboid structure with a length, width and height of 30 cm x 30 cm x 30 cm. During pyrolysis, the condensation device 3-3 is turned on to condense and wash the pyrolysis gas, that is, the pyrolysis gas produced in the pyrolysis unit 2, under the effect of heating and pressurization, enters the pyrolysis gas pipeline 3-1 through the pyrolysis unit gas outlet 2-3. The pyrolysis gas pipeline 3-1 is made of heat-resistant plastic with a diameter of 3 cm, and a gas outlet of which is connected to the condensation device 3-3. The condensation device 3-3 is a cylindrical condensation tube made of glass with a diameter of 5 cm and a length of 20 cm, a glass gas pipeline with a diameter of 2 cm is arranged in the condensation tube, a space for cooling water to flow in and out is formed in an external cylindrical annular closed cavity, and the condensation device 3-3 is connected to a tap water pipe for providing cooling water.|[0040] When the pyrolysis gas 3 enters the condensation device 3-3, a part of its components is cooled by the cooling water in the condensation device 3-3 and enter the condensate receiving device. The condensate receiving device is a cone-shaped glass bottle with a height of 8 cm and a diameter of 6 cm, and the residual exhaust gas discharge pipeline 3-5 is arranged at a side face of the condensate receiving device. After passing through the condensate receiving device 3-4, residual exhaust gas enters the exhaust gas absorption and washing device 3-6, and the exhaust gas absorption and washing device 3-6 is a cylindrical glass container with a diameter of 10 cm and a height of 8 cm, and containing 80% of the volume of tap water inside. The exhaust gas, after being absorbed and deodorized by washing liquid, enters the condensation and washing unit 3 and is discharged from the device through the condensation and washing unit gas outlet 3-2, and the condensation and washing unit gas outlet 3-2 is a plastic pipe with a diameter of 3 cm.|Embodiment 2|[0041] A use method of the household perishable garbage treatment equipment in Embodiment 1 is further proposed in the present disclosure. Firstly, perishable organic garbage is crushed, that is, the household perishable organic garbage is placed into a crushing device basket 1-2 by a user, a cover plate is arranged on a top of a crushing housing, cooling water is turned on, a crushing device 1-3 is started to crush the perishable organic garbage to a certain extent, wherein the cooling water and landfill leachate are discharged into a sewage pipe network through a cooling water and leachate outlet 1-5. Secondly, pyrolysis treatment is performed on the crushed perishable organic garbage, the crushing device basket 1-2 is taken out by the user, the crushed perishable organic garbage is poured into a pyrolysis device basket 2-1, and the pyrolysis device basket 2-1 is placed into a pyrolysis unit 2; then the pyrolysis unit and the pyrolysis device basket are filled with solid heat medium 2-2 to fully surround the crushed perishable organic garbage, and then a cover plate is arranged on a top of a pyrolysis housing, a heating plate 2-4 is started, the temperature is increased to a certain degree and kept for a period of time to achieve full pyrolysis of the perishable organic garbage. Gas produced during pyrolysis is discharged into a pyrolysis gas pipeline 3-1 through a pyrolysis unit gas outlet 2-3, and by means of structural features of the pyrolysis device basket 2-1, the solid heat medium 2-2 can be screened and separated, and pyrolytic biochar 2-5 can be collected regularly. During pyrolysis, a condensation and washing unit 3 is turned on to condense and collect low-boiling pyrolysis liquid in the pyrolysis gas, and non-condensable components of the gas are treated by an exhaust gas absorption and washing device 3-6 and discharged from the device.|[0042] It should be noted that it is apparent to those skilled in the art that the present disclosure is not limited to the details of the above exemplary embodiments, and can be realized in other specific forms without departing from the spirit or basic characteristics of the present disclosure. Therefore, the embodiments should be considered as exemplary and non-limiting in all aspects, and the scope of the present disclosure is defined by the appended claims rather than the above description, so it is intended to embrace all changes that fall within the meaning and range of equivalents of the claims, and any reference signs in the claims should not be regarded as limiting the claims involved.|[0043] Specific examples are used herein for illustration of the principles and implementations of the present disclosure. The description of the embodiments is merely used to help illustrate the method and its core principles of the present disclosure. In addition, a person of ordinary skill in the art can make various modifications in terms of specific embodiments and scope of application in accordance with the teachings of the present disclosure. In conclusion, the content of this specification shall not be construed as a limitation to the present disclosure. (US12595419)|CROSS-REFERENCE TO RELATED APPLICATION|[0001] This patent application claims the benefit and priority of Chinese Patent Application No. 202311567112.0 filed with the China National Intellectual Property Administration on Nov. 22, 2023, the disclosure of which is incorporated by reference herein in its entirety as part of the present application.|(US12595419)|TECHNICAL FIELD|[0002] The present disclosure relates to the technical field of environmental engineering, in particular to a household perishable garbage treatment equipment, and a use method thereof.|BACKGROUND|[0003] Household perishable garbage usually refers to organic solid waste produced in the daily life of urban residents, mainly including kitchen waste, garden waste, human and animal manure and so on.|[0004] Perishable garbage has the following hazards: harmful gases such as ammonia and sulfide released by the perishable garbage piled up outdoors will pollute the atmosphere and urban living environment; high-concentration leachate produced in the process of piling and spoilage will seriously pollute the water body; it is easy to breed pathogenic microorganisms, mosquitoes, flies, cockroaches, mice, and other harmful organisms, affecting the health of residents; a lot of land is occupied; and accidents such as garbage explosions may be caused. Therefore, serious harm will be caused to the lift and ecological environment of residents if urban organic waste cannot be effectively treated, and thus the treatment of urban organic waste must be paid attention to by all parties.|[0005] The traditional main treatment mode for perishable garbage mainly adopts a centralized treatment mode, that is, household garbage in a city is collected uniformly and transported to a centralized treatment plant for treatment. Common methods include composting treatment, incineration treatment, pyrolysis treatment, landfill treatment and biological treatment, etc., but the existing centralized treatment methods need to be further improved. For example, composting treatment has the disadvantages of relatively low treatment efficiency, unstable treatment process caused by different components of waste, and large floor area. Incineration treatment has the disadvantages of the risk of producing secondary pollutants such as dioxins, and waste of resources. Pyrolysis treatment has the disadvantages of strong professionalism in operation, and limited pathways for resource utilization of existing products. Landfill treatment has the disadvantages of large floor area and high removal cost. The use of biological treatment processes such as black soldier flies, earthworms and anaerobic fermentation by microorganisms has the disadvantages of relatively low conversion efficiency, great influence by climate and other environments, and large floor area.|[0006] On the other hand, with the gradual popularization and implementation of garbage sorting in cities and rural areas, requirements for sorted collection, sorted transportation and sorted treatment of household perishable garbage such as sorted kitchen waste and garden garbage have been put forward, while an independent organic garbage collection and transportation system is huge and complicated, with high cost and many problems. These problems are particularly serious in small and medium-sized counties and cities with low population density and low garbage production intensity, and the current separate treatment technology for sorted organic garbage still needs to be improved. As a result, residents sort their garbage at the source, but the sorted garbage is mixed together again by garbage removal and treatment units for removal or treatment, which greatly dampens the enthusiasm of residents to implement garbage sorting and delays the popularization and implementation of garbage sorting.|[0007] The existence of the above problems puts forward an objective demand for decentralized treatment of perishable garbage at the source, that is, the garbage is sorted at the source with families as the unit and effectively treated, which not only can solve the problems of sorted transportation and sorted treatment faced by the sorted and collected garbage at present, but also can achieve the resource utilization of products at the source, thus reducing energy consumption in the processes of centralized treatment, removal and collection, resource utilization and distribution of centrally treated products and the like. While reducing treatment cost, significant carbon emission reduction effect and obvious social and environmental benefits are achieved.|[0008] At present, the commonly used decentralized treatment technologies for organic waste in China and at abroad include kitchen waste crushing treatment technology, household composting treatment technology, earthworm reactor, water evaporation treatment equipment, small-scale pyrolysis equipment, etc. The small-scale pyrolysis decentralized treatment equipment for organic waste has attracted attention of people due to its advantages of high treatment efficiency, relatively stable process and high value of biochar resource utilization from pyrolysis products. However, generally speaking, household pyrolysis processes and equipment still have shortcomings such as a lack of basic technical theoretical support and insufficient design and development capabilities of equipment, so it is urgent to develop new treatment devices.|SUMMARY|[0009] For addressing the disadvantages in the existing household perishable garbage treatment, a novel and efficient treatment equipment and a use method thereof is proposed in the present disclosure.|[0010] To achieve the objective above, the present disclosure provides the following technical solution:|[0011] A household perishable garbage treatment equipment, including a crushing unit, a pyrolysis unit, and a condensation and washing unit.|[0012] The crushing unit includes a crushing housing, a cooling water inlet pipe, a crushing device basket, a crushing device, and a cooling water and leachate outlet. A top of the crushing housing is openable, the cooling water inlet pipe is arranged at one side of an upper part of the crushing housing, the crushing device basket is configured for containing perishable organic garbage to be crushed, the crushing device basket is arranged in the crushing housing, the crushing device is arranged in the crushing device basket, and the cooling water and leachate outlet is arranged at a bottom of the crushing housing.|[0013] The pyrolysis unit includes a pyrolysis housing, a pyrolysis device basket, solid heat medium, a pyrolysis unit gas outlet, and a heating plate. The pyrolysis device basket is arranged in the pyrolysis housing, the heating plate is arranged at a bottom of the pyrolysis housing, the solid heat medium is arranged inside both the pyrolysis housing and the pyrolysis device basket, the pyrolysis device basket is configured for containing the crushed perishable organic garbage, the pyrolysis unit gas outlet is arranged at one side of an upper part of the pyrolysis housing, and the pyrolysis unit gas outlet is in communication with the condensation and washing unit.|[0014] The condensation and washing unit includes a condensation housing, a pyrolysis gas pipeline, a condensation and washing unit gas outlet, a condensation device, a condensate receiving device, a residual exhaust gas discharge pipeline, and an exhaust gas absorption and washing device. The pyrolysis gas pipeline and the condensation and washing unit gas outlet are arranged on an upper part of the condensation housing, an end of the pyrolysis gas pipeline is in communication with the pyrolysis unit gas outlet, another end of the pyrolysis gas pipeline passes through the condensation device and is in communication with the condensate receiving device, an upper part of the condensate receiving device is in communication with an end of the residual exhaust gas discharge pipeline, and another end of the residual exhaust gas discharge pipeline extends to a bottom of the exhaust gas absorption and washing device; and the exhaust gas absorption and washing device is configured for containing condensate.|[0015] Optionally, the crushing housing, the pyrolysis housing and the condensation housing are all made of heat-resistant plastic.|[0016] Optionally, removable cover plates are arranged on the top of the crushing housing and a top of the pyrolysis housing, respectively.|[0017] Optionally, the crushing device includes a crushing blade, a blade mounting rod, and a top mounting head. The crushing blade is arranged on an outer wall of the blade mounting rod, the top mounting head is arranged on a top of the blade mounting rod, and the top mounting head is configured to be connected to a driving device.|[0018] Optionally, the crushing device basket is of a cylindrical structure with an open top, and multiple holes are evenly distributed on a surface of the crushing device basket at intervals.|[0019] Optionally, the pyrolysis device basket is of a mesh bag shaped structure with an open top, and the pyrolysis device basket is made of stainless-steel wire mesh.|[0020] Optionally, the solid heat medium is one or more of sand, kaolin, quartz sand, stone powder, yellow loam and red loam with a particle size less than 5 mm.|[0021] Optionally, the pyrolysis housing is lined with thermal insulation material inside.|[0022] Optionally, the condensate is tap water, sodium hydroxide, dilute hydrochloric acid, sodium bicarbonate, or ethanol.|[0023] A use method of a household perishable garbage treatment equipment is further proposed in the present disclosure. The method includes the following steps: firstly, crushing perishable organic garbage, that is, placing, by a user, household perishable organic garbage into a crushing device basket, arranging a cover plate on a top of a crushing housing, turning on cooling water, starting a crushing device to crush the perishable organic garbage to a certain extent, wherein cooling water and landfill leachate are discharged into a sewage pipe network through a cooling water and leachate outlet; secondly, performing pyrolysis treatment on the crushed perishable organic garbage, that is, taking out, by the user, the crushing device basket, pouring the crushed perishable organic garbage into a pyrolysis device basket, placing the pyrolysis device basket into a pyrolysis unit, filling the pyrolysis unit and the pyrolysis device basket with solid heat medium to fully surround the crushed perishable organic garbage, and then arranging a cover plate on a top of the pyrolysis housing, starting a heating plate for heating, increasing temperature to a certain degree and keeping the temperature for a period of time to achieve full pyrolysis of the perishable organic garbage, wherein gas produced during pyrolysis is exhausted into a pyrolysis gas pipeline through a pyrolysis unit gas outlet, and by means of structural features of the pyrolysis device basket, the solid heat medium is capable of being screened and separated, and pyrolysis biochar is capable of being collected regularly; and during pyrolysis, turning on a condensation and washing unit to condense and collect low-boiling pyrolysis liquid in the pyrolysis gas, wherein non-condensable components of the gas are treated by an exhaust gas absorption and washing device and discharged from the device.|[0024] Compared with the prior art, the present disclosure obtains the following beneficial technical effects:|[0025] In the present disclosure, the household perishable garbage treatment equipment and the use method thereof can effectively treat perishable garbage on the spot, reduce the collection and treatment cost required by traditional perishable garbage treatment modes, achieve carbon sequestration and resource utilization of products, and have significant economic, ecological and social benefits.|(US12595419)|BRIEF DESCRIPTION OF THE DRAWINGS|[0026] To describe the technical solutions in the embodiments of the present disclosure or in the prior art more clearly, the following briefly introduces the accompanying drawings required for describing the embodiments. Apparently, the accompanying drawings in the following description show merely some embodiments of the present disclosure, and those of ordinary skill in the art may still obtain other drawings from these accompanying drawings without creative efforts.|[0027] FIG. 1 is a schematic diagram of structure of a household perishable garbage treatment equipment according to an embodiment of the present disclosure.|(US12595419)|DETAILED DESCRIPTION|[0028] In the drawings: 1—crushing unit; 2—pyrolysis unit; 3—condensation and washing unit; 1-1—cooling water inlet pipe; 1-2—crushing device basket; 1-3—crushing device; 1-4—perishable organic garbage to be crushed; 1-5—cooling water and leachate outlet; 2-1—pyrolysis device basket; 2-2—solid heat medium; 2-3—pyrolysis unit gas outlet; 2-4—heating plate; 2-5—pyrolytic biochar; 3-1—pyrolysis gas pipeline; 3-2—condensation and washing unit gas outlet; 3-3—condensation device; 3-4—condensate receiving device; 3-5—residual exhaust gas discharge pipeline; 3-6—exhaust gas absorption and washing device.|DETAILED DESCRIPTION OF THE EMBODIMENTS|[0029] The following clearly and completely describes the technical solutions in the embodiments of the present disclosure with reference to the accompanying drawings in the embodiments of the present disclosure. Apparently, the described embodiments are merely a part rather than all of the embodiments of the present disclosure. All other embodiments obtained by a person of ordinary skill in the art based on the embodiments of the present disclosure without creative efforts shall fall within the protection scope of the present disclosure.|Embodiment 1|[0030] As shown in FIG. 1, the present embodiment provides a household perishable garbage treatment equipment, including a crushing unit 1, a pyrolysis unit 2, and a condensation and washing unit 3.|[0031] The crushing unit 1 includes a crushing housing, a cooling water inlet pipe 1-1, a crushing device basket 1-2, a crushing device 1-3, and a cooling water and leachate outlet 1-5. A top of the crushing housing is openable, the cooling water inlet pipe 1-1 is arranged at one side of an upper part of the crushing housing, the crushing device basket 1-2 is configured for containing perishable organic garbage to be crushed 1-4, the crushing device basket 1-2 is arranged in the crushing housing, the crushing device 1-3 is arranged in the crushing device basket 1-2, and the cooling water and leachate outlet 1-5 is arranged at a bottom of the crushing housing.|[0032] The pyrolysis unit 2 includes a pyrolysis housing, a pyrolysis device basket 2-1, solid heat medium 2-2, a pyrolysis unit gas outlet 2-3, and a heating plate 2-4. The pyrolysis device basket 2-1 is arranged in the pyrolysis housing, the heating plate 2-4 is arranged at a bottom of the pyrolysis housing, the solid heat medium 2-2 is arranged inside both the pyrolysis housing and the pyrolysis device basket 2-1, the pyrolysis device basket 2-1 is configured for containing the crushed perishable organic garbage, the pyrolysis unit gas outlet 2-3 is arranged at one side of an upper part of the pyrolysis housing, and the pyrolysis unit gas outlet 2-3 is in communication with the condensation and washing unit 3.|[0033] The condensation and washing unit 3 includes a condensation housing, a pyrolysis gas pipeline 3-1, a condensation and washing unit gas outlet 3-2, a condensation device 3-3, a condensate receiving device 3-4, a residual exhaust gas discharge pipeline 3-5, and an exhaust gas absorption and washing device 3-6. The pyrolysis gas pipeline 3-1 and the condensation and washing unit gas outlet 3-2 are arranged on an upper part of the condensation housing, an end of the pyrolysis gas pipeline 3-1 is in communication with the pyrolysis unit gas outlet 3-2, another end of the pyrolysis gas pipeline 3-1 passes through the condensation device 3-3 and is in communication with the condensate receiving device 3-4, an upper part of the condensate receiving device 3-4 is in communication with an end of the residual exhaust gas discharge pipeline 3-5, and another end of the residual exhaust gas discharge pipeline 3-5 extends to a bottom of the exhaust gas absorption and washing device 3-6; and the exhaust gas absorption and washing device 3-6 is configured for containing condensate.|[0034] In this specific embodiment, the crushing housing is made of heat-resistant plastic, which is of a cuboid structure with a length, width and height of 25 cm x 30 cm x 30 cm. When a cover plate is removed, the crushing device 1-3 can be installed, which includes a crushing blade, a blade mounting rod, and a top mounting head. The crushing blade is arranged on an outer wall of the blade mounting rod, and the top mounting head is arranged on a top of the blade mounting rod, and the top mounting head is configured to be connected to a driving device. The crushing blade is a propeller-shaped stainless-steel blade with a total length of 10 cm at the bottom. The crushing blade mounting rod is a stainless-steel rod with a diameter of 10 mm and a height of 15 cm. The top mounting head is connected to a power supply and can rotate the crushing blade to cut and crush perishable garbage. The crushing device basket 1-2 has a diameter of 20 cm and a height of 17 cm, and is made of stainless steel. Circular holes with a diameter of 0.5 cm are evenly distributed on a surface of the crushing device basket at intervals of 3 cm. The blade of the crushing device 1-3 is installed and fixed at the center of the crushing device basket 1-2, and thus the crushing device basket 1-2 can be hung in the crushing unit 1 by a hook.|[0035] After the crushing device basket and crushing device 1-3 are installed, the perishable garbage can be placed in the basket, then the cover plate is arranged, cooling water is turned on, and the crushing device 1-3 is started for crushing. The cooling water inlet pipe 1-1 has a diameter of 2 cm and is connected to a household tap, and a water outlet of the cooling water inlet pipe 1-1 is located above the crushing device basket 1-2. The cooling water is sprayed in a direction tangential to the rotation of the blade, thus playing a role in cooling and cleaning. During crushing, the cooling water and landfill leachate are discharged into a sewer through the cooling water and leachate outlet 1-5, and the cooling water and leachate outlet 1-5 has a diameter of 2 cm, a lower part of which is directly connected to a sewer pipe with a plastic hose.|[0036] The pyrolysis housing is made of the heat-resistant plastic. A removable cover plate is arranged on a top of the pyrolysis housing. The pyrolysis housing is of a cuboid structure with a length, width and height of 10 cm x 30 cm x 30 cm. The pyrolysis housing is lined with thermal insulation cotton inside. The cover plate can be removed from an upper part of the pyrolysis unit 2 for placing or taking out the pyrolysis device basket 2-1. The pyrolysis device basket 2-1 is of a cuboid mesh bag shaped structure with a hollow upper part and closed at periphery and bottom, and with a length, width and height of 9 cm x 28 cm x 28 cm. The mesh bag is made of stainless-steel wire mesh with a hole diameter of 5 mm. The solid heat medium 2-2 is placed in the pyrolysis unit 2, and the solid heat medium 2-2 is sand with a particle size less than 2 mm.|[0037] After the perishable garbage is crushed in the crushing unit 1, the crushing device basket 1-2 can be taken out, the crushed perishable garbage in the crushing basket is poured into the pyrolysis device basket. Then, the pyrolysis device basket 2-1 is fixed into the pyrolysis unit 2 by a hook, the periphery of the pyrolysis device basket 2-1 is filled with the solid heat medium 2-2, such that the periphery of the crushed perishable organic garbage can be fully surround by the solid heat medium 2-2. After that, the cover plate is arranged on the pyrolysis unit 2, the heating plate 2-4 is started, and after the temperature is increased to a certain degree and kept for a period of time, full pyrolysis of perishable organic garbage can be achieved. The heating plate 2-4 is installed at a bottom of the pyrolysis unit 2, with a length, width and thickness of 9 cm x 28 cm x 1 cm, and is made of a stainless-steel plate containing heat wires. During pyrolysis, when the cover plate is arranged at the upper part of the pyrolysis unit 2, the pyrolysis gas can only be discharged from the pyrolysis unit 2 through the pyrolysis unit gas outlet 2-3. The pyrolysis unit gas outlet 2-3 is a heat-resistant plastic circular tube with a diameter of 3 cm, which has a length of 2 cm inside the pyrolysis unit 2 and a mesh cover wrapped outside. The pyrolysis unit gas outlet 2-3 is connected to the pyrolysis gas pipeline 3-1 in the condensation and washing unit 3, and the produced gas is discharged into the pyrolysis gas pipeline 3-1 from the pyrolysis unit gas outlet 2-3.|[0038] After pyrolysis is finished, the pyrolysis device basket 2-1 is taken out from the pyrolysis unit 2. Under the action of gravity, the solid heat medium 2-2 with a particle size less than the mesh diameter of the pyrolysis device basket 2-1 falls from the basket, and the pyrolytic biochar 2-5 with a particle size greater than 5 mm after pyrolysis is intercepted into the basket and then taken out of the device.|[0039] The condensation housing is made of heat-resistant plastic, the condensation and washing unit 3 is of a cuboid structure with a length, width and height of 30 cm x 30 cm x 30 cm. During pyrolysis, the condensation device 3-3 is turned on to condense and wash the pyrolysis gas, that is, the pyrolysis gas produced in the pyrolysis unit 2, under the effect of heating and pressurization, enters the pyrolysis gas pipeline 3-1 through the pyrolysis unit gas outlet 2-3. The pyrolysis gas pipeline 3-1 is made of heat-resistant plastic with a diameter of 3 cm, and a gas outlet of which is connected to the condensation device 3-3. The condensation device 3-3 is a cylindrical condensation tube made of glass with a diameter of 5 cm and a length of 20 cm, a glass gas pipeline with a diameter of 2 cm is arranged in the condensation tube, a space for cooling water to flow in and out is formed in an external cylindrical annular closed cavity, and the condensation device 3-3 is connected to a tap water pipe for providing cooling water.|[0040] When the pyrolysis gas 3 enters the condensation device 3-3, a part of its components is cooled by the cooling water in the condensation device 3-3 and enter the condensate receiving device. The condensate receiving device is a cone-shaped glass bottle with a height of 8 cm and a diameter of 6 cm, and the residual exhaust gas discharge pipeline 3-5 is arranged at a side face of the condensate receiving device. After passing through the condensate receiving device 3-4, residual exhaust gas enters the exhaust gas absorption and washing device 3-6, and the exhaust gas absorption and washing device 3-6 is a cylindrical glass container with a diameter of 10 cm and a height of 8 cm, and containing 80% of the volume of tap water inside. The exhaust gas, after being absorbed and deodorized by washing liquid, enters the condensation and washing unit 3 and is discharged from the device through the condensation and washing unit gas outlet 3-2, and the condensation and washing unit gas outlet 3-2 is a plastic pipe with a diameter of 3 cm.|Embodiment 2|[0041] A use method of the household perishable garbage treatment equipment in Embodiment 1 is further proposed in the present disclosure. Firstly, perishable organic garbage is crushed, that is, the household perishable organic garbage is placed into a crushing device basket 1-2 by a user, a cover plate is arranged on a top of a crushing housing, cooling water is turned on, a crushing device 1-3 is started to crush the perishable organic garbage to a certain extent, wherein the cooling water and landfill leachate are discharged into a sewage pipe network through a cooling water and leachate outlet 1-5. Secondly, pyrolysis treatment is performed on the crushed perishable organic garbage, the crushing device basket 1-2 is taken out by the user, the crushed perishable organic garbage is poured into a pyrolysis device basket 2-1, and the pyrolysis device basket 2-1 is placed into a pyrolysis unit 2; then the pyrolysis unit and the pyrolysis device basket are filled with solid heat medium 2-2 to fully surround the crushed perishable organic garbage, and then a cover plate is arranged on a top of a pyrolysis housing, a heating plate 2-4 is started, the temperature is increased to a certain degree and kept for a period of time to achieve full pyrolysis of the perishable organic garbage. Gas produced during pyrolysis is discharged into a pyrolysis gas pipeline 3-1 through a pyrolysis unit gas outlet 2-3, and by means of structural features of the pyrolysis device basket 2-1, the solid heat medium 2-2 can be screened and separated, and pyrolytic biochar 2-5 can be collected regularly. During pyrolysis, a condensation and washing unit 3 is turned on to condense and collect low-boiling pyrolysis liquid in the pyrolysis gas, and non-condensable components of the gas are treated by an exhaust gas absorption and washing device 3-6 and discharged from the device.|[0042] It should be noted that it is apparent to those skilled in the art that the present disclosure is not limited to the details of the above exemplary embodiments, and can be realized in other specific forms without departing from the spirit or basic characteristics of the present disclosure. Therefore, the embodiments should be considered as exemplary and non-limiting in all aspects, and the scope of the present disclosure is defined by the appended claims rather than the above description, so it is intended to embrace all changes that fall within the meaning and range of equivalents of the claims, and any reference signs in the claims should not be regarded as limiting the claims involved.|[0043] Specific examples are used herein for illustration of the principles and implementations of the present disclosure. The description of the embodiments is merely used to help illustrate the method and its core principles of the present disclosure. In addition, a person of ordinary skill in the art can make various modifications in terms of specific embodiments and scope of application in accordance with the teachings of the present disclosure. In conclusion, the content of this specification shall not be construed as a limitation to the present disclosure. Family Number|(108074209)|108074209|Abstract|(CN117358724 A)|The invention discloses household perishable garbage treatment equipment and a use method thereof , and relates to the technical field of environmental engineering , and the household perishable garbage treatment equipment comprises a crushing unit , a pyrolysis unit and a condensation washing unit . The perishable garbage is crushed through the crushing unit , the crushed perishable garbage is pyrolyzed into pyrolysis biochar through the pyrolysis unit , and gas generated in the pyrolysis process is condensed and collected through the condensation washing unit . According to the domestic perishable garbage treatment equipment and the using method thereof , perishable garbage can be effectively treated on site , the collection and treatment cost required by a traditional perishable garbage treatment mode is reduced , carbon sequestration and product recycling can be achieved , and the domestic perishable garbage treatment equipment and the using method thereof have good economic benefits and obvious ecological benefits and social benefits . |(US12595419 B2)|A household perishable garbage treatment equipment and a use method thereof are provided, relating to the technical field of environmental engineering. The equipment includes a crushing unit, a pyrolysis unit, and a condensation and washing unit. Perishable garbage is crushed by the crushing unit, then the crushed perishable garbage is pyrolyzed into pyrolytic biochar by the pyrolysis unit, and gas produced in the pyrolysis process is condensed and collected by the condensation and washing unit. The household perishable garbage treatment equipment and the use method thereof can effectively treat perishable garbage on the spot, reduce the collection and treatment cost required by traditional perishable garbage treatment modes, achieve carbon sequestration and resource utilization of products, and have significant economic, ecological and social benefits.|(JP7719532 B2)|PROBLEM TO BE SOLVED: To provide household perishable garbage treatment equipment and a use method thereof.SOLUTION: There are disclosed household perishable garbage treatment equipment and a use method thereof relating to a technical field of environmental engineering. The equipment includes a crushing unit 1, a pyrolysis unit 2, and a condensation and washing unit 3. Perishable garbage is crushed by the crushing unit, then the crushed perishable garbage is pyrolyzed into pyrolytic bio-char by the pyrolysis unit, and gas produced in the pyrolysis process is condensed and collected by the condensation and washing unit. The household perishable garbage treatment equipment and the use method thereof can effectively treat perishable garbage on a current spot, reduce collection and treatment costs required by conventional perishable garbage treatment modes, achieve carbon sequestration and resource utilization of products, and have favorable economic, ecological and social benefits.SELECTED DRAWING: Figure 1COPYRIGHT: (C)2025,JPO&INPIT|CPC codes|(CN117358724 A)|B01D - 053/18 |(US12595419 B2)|B01D-053/18|(JP7719532 B2)|B01D-053/18|IPC codes|(US12595419 B2)|B01D-053/18|(JP7719532 B2)|B01D-053/38|B01D-053/78| Basic materials chemistry|Environmental technology B01D-053/18|B09B-003/00|B09B-003/35|B09B-003/40|B09B-2101/25|B09B-2101/70|C10B-047/06|C10B-053/00 B01D-053/18|B09B-003/00|B09B-003/35|B09B-003/40|B09B-2101/25|B09B-2101/70|C10B-047/06|C10B-053/00 B01D-053/18|B01D-053/38|B01D-053/78|B09B-003/00|B09B-003/35|B09B-003/40|B09B-101/25|B09B-101/70|C10B-047/06|C10B-053/00 B01D-053/18|B01D-053/38|B01D-053/78|B09B-003/00|B09B-003/35|B09B-003/40|B09B-101/25|B09B-101/70|C10B-047/06|C10B-053/00 JP7777254 JP7777254 116809525 WHO=Examiner SELF=N CAT=A JP2017534745|US6051110|WO2018186806|US20080307703|US20160122674|US6051110|US12303827|US20230173503|US11879106|US20210122989|US10738255|US11458414|US20080307703|US20080014112|US5980823 JP2017534745 72818510 WHO=Examiner SELF=N CAT=Y|US6051110 43123193 WHO=Examiner SELF=N CAT=Y|WO2018186806 81593423 WHO=Examiner SELF=N CAT=A|US20080307703 43740307 WHO=Examiner SELF=N CAT=A|US20160122674 72818510 WHO=Examiner SELF=N CAT=103|US6051110 43123193 WHO=Examiner SELF=N CAT=103|US12303827 104640215 WHO=Examiner SELF=N|US20230173503 96316027 WHO=Examiner SELF=N|US11879106 72818510 WHO=Examiner SELF=N|US20210122989 72818510 WHO=Examiner SELF=N|US10738255 72818510 WHO=Examiner SELF=N|US11458414 69063826 WHO=Examiner SELF=N|US20080307703 43740307 WHO=Examiner SELF=N|US20080014112 1822245 WHO=Examiner SELF=N|US5980823 13650681 WHO=Examiner SELF=N US20160122674; US6051110; US5980823; US10738255; US11458414; US11879106; US12303827; US20080014112; US20080307703; US20210122989; US20230173503|JP2017534745; US6051110; WO2018186806; US20080307703| GRANTED (US12595419)|GRANTED|(JP7719532)|GRANTED|(CN117358724)|PENDING ALIVE (US12595419)|ALIVE|(JP7719532)|ALIVE|(CN117358724)|ALIVE (US12595419)|LEGAL DETAILS FOR US12595419|Actual or expected expiration date=2044-08-31|Legal state=ALIVE|Status=GRANTED|Event publication date=2024-01-09|Event code=US/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=US US18408544|Application date=2024-01-09|Standardized application number=2024US-18408544|Event publication date=2024-01-09|Event code=US/EXMR|Event group=Administrative notifications|USPTO Examiner Name|PRIMARY EXAMINER:MILLER, JONATHAN|Event publication date=2024-01-09|Event code=US/ART|Event group=Administrative notifications|USPTO Art Group|ART=1772|Event publication date=2024-01-09|Event code=US/DK|Event group=Examination events|Attorney Docket Number|Docket Nbr: 82083-000033-US|Event publication date=2024-01-09|Event code=US/CUST|Event group=Examination events|Attorney/Agent Customer Number|Customer Nbr: 116025|Event publication date=2024-01-09|Event code=US/SMALL|Event group=Administrative notifications|Appl Has Filed a Verified Statement of Micro to Small Entity Status|Business Entity Status: Small|Event publication date=2024-01-09|Event code=US/AIA|Event group=Administrative notifications|First Inventor File Indicated:|AIA=Yes|Event publication date=2024-01-09|Event code=US/AS|Event group=Change of name or address Reassignment|Assignment|ASSIGNMENT OF ASSIGNORS INTEREST|Assignors:ZHENG, XIANGYONG;MA, PING;ZHAO, MIN;AND OTHERS|Reel/frame:066072/0087|OWNER:WENZHOU UNIVERSITY, CHINA|Effective date of the event=2023-12-28|Event publication date=2024-01-09|Event code=US/PTARDY|Event indicator=Pos|Event group=Examination events|Patent Term Adjustment - Ready for Examination|Event publication date=2024-01-09|Event code=US/ENT|Event group=Administrative notifications|Entity Status Set to Undiscounted|Event publication date=2024-01-23|Event code=US/SMALL|Event group=Administrative notifications|Appl Has Filed a Verified Statement of Micro to Small Entity Status|Event publication date=2024-01-25|Event code=US/APPFILEREC|Event group=Administrative notifications OAO|Filing Receipt|Event publication date=2024-02-01|Event code=US/AS|Event group=Change of name or address Reassignment|Assignment|CORRECTIVE ASSIGNMENT TO CORRECT THE CITY OF ASSIGNEE PREVIOUSLY RECORDED AT REEL: 066072 FRAME: 0087. ASSIGNOR(S) HEREBY CONFIRMS THE ASSIGNMENT|Assignors:ZHENG, XIANGYONG;MA, PING;ZHAO, MIN;AND OTHERS|Reel/frame:066404/0368|OWNER:WENZHOU UNIVERSITY, CHINA|Effective date of the event=2023-12-28|Event publication date=2024-02-05|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2025-05-22|Event code=US/A1|Event group=Examination events|Application published|Publication country=US|Publication number=US20250163330|Publication stage code=A1|Publication date=2025-05-22|Standardized publication number=US20250163330|Event publication date=2025-05-22|Event code=US/PGPUBN|Event indicator=Pos|Event group=Examination events OAO|PG-Pub Issue Notification|Event publication date=2025-09-21|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2025-10-28|Event code=US/CTNF|Event group=Examination events OA OAO|Non-Final Rejection|Event publication date=2025-10-30|Event 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REGISTRATION OF UTILITY MODEL|Japanese intermediate code: R150|(CN117358724)|LEGAL DETAILS FOR CN117358724|Actual or expected expiration date=2043-11-22|Legal state=ALIVE|Status=PENDING|Event publication date=2023-11-22|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202311567112|Application date=2023-11-22|Standardized application number=2023CN-1567112|Event publication date=2024-01-09|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN117358724|Publication stage code=A|Publication date=2024-01-09|Standardized publication number=CN117358724|Event publication date=2024-01-09|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-01-26|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (US12595419)|US|(JP7719532)|JP|(CN117358724)|CN 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CN; CN; CN; CN; CN; CN; CN; CN|(US20250163330)|CN; CN; CN; CN; CN; CN; CN; CN; CN; CN; CN; CN||| (US12595419)|NAME=Zheng Xiangyong, CITY=Wenzhou City, COUNTRY=CN |NAME=Ma Ping, CITY=Wenzhou City, COUNTRY=CN |NAME=Zhao Min, CITY=Wenzhou City, COUNTRY=CN |NAME=Zhu Wencong, CITY=Wenzhou City, COUNTRY=CN |NAME=Jiang Shunfeng, CITY=Wenzhou City, COUNTRY=CN |NAME=Wang Zhiquan, CITY=Wenzhou City, COUNTRY=CN |NAME=Jin Huachang, CITY=Wenzhou City, COUNTRY=CN |NAME=Wu Suqing, CITY=Wenzhou City, COUNTRY=CN |NAME=Jin Zhan, CITY=Wenzhou City, COUNTRY=CN |NAME=Bei Ke, CITY=Wenzhou City, COUNTRY=CN |NAME=Xu Bentuo, CITY=Wenzhou City, COUNTRY=CN |NAME=Kong Hainan, CITY=Wenzhou City, COUNTRY=CN|(US20250163330)|NAME=ZHENG Xiangyong, CITY=Wenzhou City, COUNTRY=CN |NAME=MA Ping, CITY=Wenzhou City, COUNTRY=CN |NAME=ZHAO Min, CITY=Wenzhou City, COUNTRY=CN |NAME=ZHU Wencong, CITY=Wenzhou City, COUNTRY=CN |NAME=JIANG Shunfeng, CITY=Wenzhou City, COUNTRY=CN |NAME=WANG Zhiquan, CITY=Wenzhou City, COUNTRY=CN |NAME=JIN Huachang, CITY=Wenzhou City, COUNTRY=CN |NAME=WU Suqing, CITY=Wenzhou City, COUNTRY=CN |NAME=JIN Zhan, CITY=Wenzhou City, COUNTRY=CN |NAME=BEI Ke, CITY=Wenzhou City, COUNTRY=CN |NAME=XU Bentuo, CITY=Wenzhou City, COUNTRY=CN |NAME=KONG Hainan, CITY=Wenzhou City, COUNTRY=CN|(JP7719532)|NAME=MA PING|NAME=CHO SATOSHI|NAME=ZHU WENCONG|NAME=JIANG SHUNFENG|NAME=WANG ZHIQUAN|NAME=JIN HUACHANG|NAME=WU SUQING|NAME=JIN Zhan|NAME=BEI KE|NAME=XU BENTUO|NAME=KOU KAINAN|(JP2025084647)|NAME=ZHENG XIANG YONG|NAME=MA PING|NAME=ZHAO MIN|NAME=ZHU WENCONG|NAME=JIANG SHUNFENG|NAME=WANG ZHIQUAN|NAME=JIN HUACHANG|NAME=WU SUQING|NAME=JIN ZHAN|NAME=BEI KE|NAME=XU BENTUO|NAME=KOU KAINAN|(CN117358724)|NAME=ZHENG XIANGYONG|NAME=MA PING|NAME=ZHAO MIN|NAME=ZHU WENCONG|NAME=JIANG SHUNFENG|NAME=WANG ZHIQUAN|NAME=JIN HUAZHANG|NAME=WU SUQING|NAME=JIN ZHAN|NAME=BEI KE|NAME=XU BENTUO|NAME=KONG HAINAN 2 3 Titre: (US12595419)|Household perishable garbage treatment equipment and use method thereof Résumé: (US12595419)|A household perishable garbage treatment equipment and a use method thereof are provided, relating to the technical field of environmental engineering. The equipment includes a crushing unit, a pyrolysis unit, and a condensation and washing unit. Perishable garbage is crushed by the crushing unit, then the crushed perishable garbage is pyrolyzed into pyrolytic biochar by the pyrolysis unit, and gas produced in the pyrolysis process is condensed and collected by the condensation and washing unit. The household perishable garbage treatment equipment and the use method thereof can effectively treat perishable garbage on the spot, reduce the collection and treatment cost required by traditional perishable garbage treatment modes, achieve carbon sequestration and resource utilization of products, and have significant economic, ecological and social benefits. 62 Abstract gpt-4o-mini no The article focuses on the treatment of household perishable garbage through pyrolysis and biochar production, which does not relate to accelerated weathering or CO₂ capture through mineral alteration.
62 CN201010181711 CN201010181711 CN101837996|CN101837996 7093988 CN101837996 B 2011-09-21 [CN101837996B]|CN101837996 A 2010-09-22 [CN101837996] 2010-05-25 2010-05-25 2011-09-21|2010-09-22 (CN101837996B)|2011-09-21 (CN101837996)|2014-07-16 (CN101837996)|Method for melting purification of magnesia by using waste magnesium product (CN101837996)|The invention relates to a method for the melting purification of magnesia by using a waste magnesium product. The adopted technical scheme is that the method comprises the following steps of: manually picking out and removing impurities visible to the naked eye from various purchased waste magnesium products; crushing and grinding the waste magnesium products subjected to the impurity removal into powder of below 800 meshes and removing iron with an iron removing device; removing carbon from the powder subjected to the iron removal by the water floatation method; loading the powder subjectedto the carbon removal by the water floatation method into a kiln bogie, conveying the kiln bogie loaded with the powder to a tunnel kiln or a shuttle kiln, closing the kiln door, stirring the powder at the temperature of 550 to 650 DEG C and blowing in oxygen for 2 to 4 hours; uniformly mixing the powder subjected to the carbon removal with light burnt magnesium powder in a weight ratio of 1:2-4 and performing compression molding and drying; conveying the dried blank to a high-temperature electric arc furnace for melting at the temperature of 2,500 to 3,500 DEG C for 6 to 8 hours; and cooling, crushing and selecting the products. The method has the advantages of saving resource, protecting environment and saving energy. DASHIQIAO WEIMING FURNACE MATERIAL (CN101837996)|DASHIQIAO WEIMING FURNACE MATERIAL Co.,Ltd.|(CN101837996)|DASHIQIAO WEIMING FURNACE MATERIAL Co.,Ltd. WANG XI|ZHU YONGZHENG (CN101837996)|WANG XI|ZHU YONGZHENG|(CN101837996)|WANG XI|ZHU YONGZHENG (CN101837996)|JIN CHUNHUA;SHENYANG JACK INTELLECTUAL PROPERTY AGENT LTD. (CN101837996)|1. A method for melting and purifying magnesia by using waste magnesium products is characterized by comprising the following steps: (1) selecting raw materials: manually selecting various purchased waste magnesium products to remove macroscopic impurities; (2) crushing and deironing: crushing and finely grinding the waste magnesium products after the impurities are removed into fine powder below 800 meshes, and removing iron by using iron removal equipment; (3) flotation and carbon removal: removing carbon from the iron-removed fine powder by a water flotation method; (4) medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car, feeding the fine powder into a tunnel kiln or a shuttle kiln, closing a kiln door, stirring at 550-650 ℃, and blowing in oxygen for 2-4 hours; (5) and (3) green compact forming and drying: uniformly mixing the fine powder subjected to carbon removal and light-burned magnesium powder according to the weight ratio of 1: 2-4, and performing green pressing and forming and drying; (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 6-8 hours at 2500-3500 ℃; (7) and cooling, crushing and sorting the product.| (CN101837996)|In order to solve the problems, the invention provides a method for melting and purifying magnesia by fully utilizing waste magnesium products, which not only saves resources, but also protects the environment. In order to achieve the purpose, the invention adopts the technical scheme that: a method for melting and purifying magnesia by using waste magnesium products comprises the following steps:|The invention relates to a method for melting and purifying magnesia by using waste magnesium products.|The invention relates to a preparation method of magnesia, in particular to a method for melting and purifying magnesia by using waste magnesium products.| (CN101837996)|MELTING(100,19)|WASTE MAGNESIUM PRODUCT(100,18)|MAGNESIA(100,13)|MACROSCOPIC IMPURITY(68,5)|FINE POWDER(64,27)|SHUTTLE KILN(63,5)|PURCHASED WASTE MAGNESIUM PRODUCT(56,3)|KILN DOOR(50,6)|REMOVING CARBON(49,22)|KILN CAR(48,9)|GREEN PRESSING(47,3)|LADLE FURNACE LINING BRICK(45,8)|CRUSHING(44,17)|WATER FLOTATION(40,4)|DRIED BLANK(39,6)|FLOTATION(35,13)|TUNNEL KILN(32,4)|IRON REMOVAL EQUIPMENT(29,6)|GREEN COMPACT(28,5)|BLOWING(28,3)|LIGHT BURNED MAGNESIUM(28,3)|IMPURITY(27,11)|IRON REMOVAL(27,9)|DEIRONING(23,5)|WASTE MAGNESIA CARBON BRICK(21,6)|BRICK LINING(20,8)|IRON REMOVED FINE(17,3)|WEIGHT RATIO(15,6)|LADLE EXPERIMENT(14,4)|TANGSHAN STAINLESS STEEL FACTORY(14,4)|DECARBURIZED FINE POWDER(14,3)|PURCHASED WASTE MAGNESIA BRICK(13,1)|ELECTRICAL ARC FURNACE(12,7)|GRAVIMETRIC COMBUSTION(12,2)|WASTE MAGNESITE BRICK(11,1)|MAGNESIA FUSION(10,3)|MAGNESIA ALUMINA CARBON BRICK(9,1)|MAGNESIUM ORE RESOURCE(9,1)|BLOWING OXYGEN(8,3)|PREPARED MAGNESIA(8,3)|WATER FLOATATION(8,3)|ELECTRIC SMELTING MAGNESITE(8,1)|MAGNESIA SAND QUALITY(8,1)|RECYCLED WASTE MAGNESIA CARBON(8,1)|RESOURCE CYCLICAL UTILIZATION(8,1)|MEDIUM TEMPERATURE CARBON REMOVAL(7,5)|LINING BRICK(7,1)|MAGNESIA SINK(7,1)|FINE POWDER CARBON CONTENT(6,3)|LIGHT BURNED MAGNESIUM POWDER(6,3)|ALUMINUM METAL ADDITIVE(6,1)|EXPIRED SPENT PRODUCT(6,1)|MAGNESIA PRODUCT MANUFACTURER(6,1)|PRODUCING MAGNESIA ALUMINA SPINEL(6,1)|RESOURCE SAVING(6,1)|MAGNESIUM OXIDE CONTENT(4,3)|CARBON FLOAT(4,1)|DECARBURIZATION RATE(4,1)|MAGNESIUM PRODUCTION MANUFACTURING(4,1)|REMOVING IMPURITY(4,1)|RESOURCE MINERAL PRODUCT(4,1)|STEEL COUNTRY(4,1)|WASTE MAGNESIUM PRODUCT MANUFACTURER(4,1)|ALUMINUM CONTENT(3,1)||(CN101837996)|MELTING(100,19)|WASTE MAGNESIUM PRODUCT(100,18)|MAGNESIA(100,13)|MACROSCOPIC IMPURITY(68,5)|FINE POWDER(64,27)|SHUTTLE KILN(63,5)|PURCHASED WASTE MAGNESIUM PRODUCT(56,3)|KILN DOOR(50,6)|REMOVING CARBON(49,22)|KILN CAR(48,9)|GREEN PRESSING(47,3)|LADLE FURNACE LINING BRICK(45,8)|CRUSHING(44,17)|DRIED BLANK(39,6)|WATER FLOTATION(39,4)|FLOTATION(35,13)|TUNNEL KILN(31,4)|IRON REMOVAL EQUIPMENT(29,6)|GREEN COMPACT(28,5)|BLOWING(28,3)|LIGHT BURNED MAGNESIUM(28,3)|IMPURITY(27,11)|IRON REMOVAL(27,9)|DEIRONING(23,5)|WASTE MAGNESIA CARBON BRICK(21,6)|BRICK LINING(20,8)|IRON REMOVED FINE(17,3)|WEIGHT RATIO(15,6)|LADLE EXPERIMENT(14,4)|TANGSHAN STAINLESS STEEL FACTORY(14,4)|DECARBURIZED FINE POWDER(14,3)|PURCHASED WASTE MAGNESIA BRICK(13,1)|ELECTRICAL ARC FURNACE(12,7)|GRAVIMETRIC COMBUSTION(12,2)|WASTE MAGNESITE BRICK(11,1)|MAGNESIA FUSION(10,3)|MAGNESIA ALUMINA CARBON BRICK(9,1)|MAGNESIUM ORE RESOURCE(9,1)|BLOWING OXYGEN(8,3)|PREPARED MAGNESIA(8,3)|WATER FLOATATION(8,3)|ELECTRIC SMELTING MAGNESITE(8,1)|MAGNESIA SAND QUALITY(8,1)|RECYCLED WASTE MAGNESIA CARBON(8,1)|RESOURCE CYCLICAL UTILIZATION(8,1)|MEDIUM TEMPERATURE CARBON REMOVAL(7,5)|LINING BRICK(7,1)|MAGNESIA SINK(7,1)|FINE POWDER CARBON CONTENT(6,3)|LIGHT BURNED MAGNESIUM POWDER(6,3)|ALUMINUM METAL ADDITIVE(6,1)|EXPIRED SPENT PRODUCT(6,1)|MAGNESIA PRODUCT MANUFACTURER(6,1)|PRODUCING MAGNESIA ALUMINA SPINEL(6,1)|RESOURCE SAVING(6,1)|MAGNESIUM OXIDE CONTENT(4,3)|CARBON FLOAT(4,1)|DECARBURIZATION RATE(4,1)|MAGNESIUM PRODUCTION MANUFACTURING(4,1)|REMOVING IMPURITY(4,1)|RESOURCE MINERAL PRODUCT(4,1)|STEEL COUNTRY(4,1)|WASTE MAGNESIUM PRODUCT MANUFACTURER(4,1)|ALUMINUM CONTENT(3,1)| (CN101837996)|1. A method for melting and purifying magnesia by using waste magnesium products is characterized by comprising the following steps:|(1) selecting raw materials: manually selecting various purchased waste magnesium products to remove macroscopic impurities;|(2) crushing and deironing: crushing and finely grinding the waste magnesium products after the impurities are removed into fine powder below 800 meshes, and removing iron by using iron removal equipment;|(3) flotation and carbon removal: removing carbon from the iron-removed fine powder by a water flotation method;|(4) medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car, feeding the fine powder into a tunnel kiln or a shuttle kiln, closing a kiln door, stirring at 550-650 ℃, and blowing in oxygen for 2-4 hours;|(5) and (3) green compact forming and drying: uniformly mixing the fine powder subjected to carbon removal and light-burned magnesium powder according to the weight ratio of 1: 2-4, and performing green pressing and forming and drying;|(6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 6-8 hours at 2500-3500 ℃;|(7) and cooling, crushing and sorting the product. (CN101837996)|TECHNICAL FIELD|[0002] The invention relates to a preparation method of magnesia, in particular to a method for melting and purifying magnesia by using waste magnesium products.|BACKGROUND ART|[0004] The basic refractory material is a necessary product in industries such as steel, cement and the like, the main raw material of the basic refractory material is magnesia, although the magnesium ore resource in China is rich, the basic refractory material is a resource mineral product, and one part is less when being exploited, so the use of the basic refractory material needs to be reasonably planned. However, at present, the use of the alkaline refractory materials is basically disposable, the waste magnesia carbon bricks, magnesia bricks and the like are basically treated as garbage, and although the waste magnesia carbon bricks are also recycled at present, the recycled waste magnesia carbon bricks are used as waste materials and cannot be used for producing high-grade magnesia products, so that the waste of mineral resources is caused.|[0005] China is a large industrial country, a large iron and steel country, and more than ten million waste magnesia carbon bricks, the recycling of waste magnesia carbon bricks is struggled, and magnesia is a mineral resource and cannot be regenerated, so that the full utilization of waste magnesium products is imperative from the strategic point of long-term development.|DISCLOSURE|[0006] Disclosure of Invention|[0007] In order to solve the problems, the invention provides a method for melting and purifying magnesia by fully utilizing waste magnesium products, which not only saves resources, but also protects the environment.|[0008] In order to achieve the purpose, the invention adopts the technical scheme that: a method for melting and purifying magnesia by using waste magnesium products comprises the following steps:|[0009] (1) selecting raw materials: manually selecting various purchased waste magnesium products to remove macroscopic impurities;|[0010] generally, the main raw materials of waste magnesium products purchased are: used waste magnesia carbon bricks, magnesia bricks or expired and failed products of magnesia product manufacturers and the like.|[0011] The magnesia carbon brick and the magnesia brick are used, and impurities such as aluminum, iron, calcium and the like which are different from the brick are obviously remained on the surfaces of the magnesia carbon brick and the magnesia brick, so that the impurities are firstly removed manually when raw materials are selected, the high-temperature melting time is shortened, and the production cost is reduced.|[0012] (2) Crushing and deironing: crushing and finely grinding the waste magnesium products after the impurities are removed into fine powder below 800 meshes, and removing iron by using iron removal equipment;|[0013] (3) flotation and carbon removal: removing carbon from the iron-removed fine powder by a water flotation method;|[0014] (4) medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car, feeding the fine powder into a tunnel kiln or a shuttle kiln, closing a kiln door, stirring at 550-650 ℃, and blowing in oxygen for 2-4 hours;|[0015] (5) and (3) green compact forming and drying: uniformly mixing the fine powder subjected to carbon removal and light-burned magnesium powder according to the weight ratio of 1: 2-4, and performing green pressing and forming and drying;|[0016] (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 6-8 hours at 2500-3500 ℃;|[0017] (7) and cooling, crushing and sorting the product.|[0018] In the invention, impurities in waste magnesium products such as phosphate, resin and the like can be decomposed and volatilized in a high-temperature melting state, and the impurity which is least easy to remove is carbon.|[0019] The physical and chemical indexes of the magnesite prepared by the method are shown in Table 1.|[0020] TABLE 1|Index (I)97 electric smelting magnesiteMagnesite prepared by the method of the invention SiO2 % 1.13 ≤1.25 Al2O3 % 0.10 ≤0.3 Fe2O3 % 0.80 ≤1.0 CaO % 1.08 ≤1.2 MgO % 96.81 ≥96 IL 0.08 ≤0.12 B.D 3.48 ≤3.49 |[0022] It can be seen from table 1 that the magnesite prepared by the method of the present invention has a slightly lower purity than normal fused magnesite, but does not affect the use of magnesite because the content of alumina in the magnesite is higher. The method mainly depends on raw materials, recycled waste magnesia carbon bricks often contain metallic aluminum additives, and part of magnesia carbon bricks are likely to be mixed in the raw materials, so that the aluminum content of products is higher, the quality of magnesia sand is not influenced when alumina and magnesia are used for producing magnesia-alumina spinel in a high-temperature molten state, and the magnesia sand of the products is mainly used in the following aspects: the production of metallurgical refractory materials such as magnesia carbon bricks, magnesia alumina carbon bricks, magnesia bricks, ladle castable, tundish coating materials, electric furnace bottom ramming materials and the like has good effect, low production cost and cyclic utilization of resources, and accords with the national conditions of China. The magnesite prepared by the method is pressed into the lining brick of the ladle furnace, and after three ladle experiments in Tangshan stainless steel factories, the lining brick has no obvious difference in use compared with the lining brick of the ladle furnace prepared by common fused magnesite.|[0023] The invention has the beneficial effects that: saving resources and protecting environment. The invention makes full use of various waste magnesium products, such as waste magnesia carbon bricks, magnesia bricks or expired spent products of magnesium product manufacturers, and recycles the existing magnesia to the maximum extent. And secondly, energy is saved. Most of macroscopic impurities are removed through manual selection, and the high-temperature melting time is shortened. Secondly, the melting time of the electric arc furnace is directly influenced by the decarburization rate, namely the cost, and the direct hook is economical.|INVENTION MODE|[0024] Detailed Description|[0025] Example 1 method for purifying magnesite by melting waste magnesia carbon bricks|[0026] The method comprises the following steps:|[0027] (1) selecting raw materials: manually selecting and removing impurities such as aluminum, iron, calcium and the like which can be seen by naked eyes from purchased waste magnesia carbon bricks;|[0028] (2) crushing and deironing: crushing and finely grinding the waste magnesia carbon bricks after the impurities are removed into fine powder below 800 meshes, and removing iron by iron removal equipment;|[0029] (3) flotation and carbon removal: and (3) placing the fine powder subjected to iron removal in a water tank, and removing carbon by a water floatation method. The carbon floats on the water surface and the magnesia sinks at the water bottom by utilizing the different specific gravity of the carbon and the magnesia, so that most of the carbon is removed;|[0030] the carbon content of the fine powder after water flotation is 5 percent by measuring the total carbon content by adopting a combustion gravimetric method (the execution standard is GB/T13245-91).|[0031] (4) Medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car (a raw material stirring device is arranged on the kiln car), feeding the fine powder into a tunnel kiln, closing a kiln door, stirring at 550-650 ℃, and blowing oxygen for 3 hours;|[0032] (5) and (3) green compact forming and drying: uniformly mixing the decarburized fine powder and light-burned magnesium powder (the content of magnesium oxide is 97%) according to the weight ratio of 1: 3, and performing green pressing, forming and drying;|[0033] (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 7 hours at 3000 ℃;|[0034] (5) cooling, crushing and sorting the product.|[0035] The results are shown in Table 2. The prepared magnesia is further pressed into the lining brick of the ladle furnace, and after three ladle experiments in a Tangshan stainless steel factory, the lining brick of the ladle furnace has no obvious difference in use compared with the lining brick of the ladle furnace made of common fused magnesia.|[0036] Example 2 method for melting and purifying magnesite by using waste magnesite bricks|[0037] The method comprises the following steps:|[0038] (1) selecting raw materials: manually selecting and removing impurities such as aluminum, iron, calcium and the like which can be seen by naked eyes from purchased waste magnesia bricks;|[0039] (2) crushing and deironing: crushing and finely grinding the waste magnesia bricks after the impurities are removed into fine powder below 800 meshes, and removing iron by using iron removal equipment;|[0040] (3) flotation and carbon removal: and (3) placing the fine powder subjected to iron removal in a water tank, and removing carbon by a water floatation method.|[0041] The carbon content of the fine powder after flotation was 5% as determined by gravimetric combustion determination (the standard being applied is GB/T13245-91).|[0042] (4) Medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car (a raw material stirring device is arranged on the kiln car), conveying the fine powder into a shuttle kiln, closing a kiln door, stirring at 550-650 ℃, and blowing oxygen for 4 hours;|[0043] (5) and (3) green compact forming and drying: uniformly mixing the decarburized fine powder and light-burned magnesium powder (the content of magnesium oxide is 97.5%) according to the weight ratio of 1: 4, and performing green pressing, forming and drying;|[0044] (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 7 hours at 3000 ℃;|[0045] (5) cooling, crushing and sorting the product.|[0046] The results are shown in Table 2. The prepared magnesia is further pressed into the lining brick of the ladle furnace, and after three ladle experiments in a Tangshan stainless steel factory, the lining brick of the ladle furnace has no obvious difference in use compared with the lining brick of the ladle furnace made of common fused magnesia.|[0047] Example 3 method for melting and purifying magnesite by using waste magnesium product|[0048] The method comprises the following steps:|[0049] (1) selecting raw materials: manually selecting expired and failed magnesium products of purchased waste magnesium product manufacturers to remove macroscopic impurities;|[0050] (2) crushing and deironing: crushing and finely grinding the waste magnesium product after removing impurities into fine powder below 800 meshes, and removing iron by using iron removal equipment;|[0051] (3) flotation and carbon removal: and (3) placing the fine powder subjected to iron removal in a water tank, and removing carbon by a water floatation method.|[0052] The carbon content of the fine powder after flotation was 5% as determined by gravimetric combustion determination (the standard being applied is GB/T13245-91).|[0053] (4) Medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car (a raw material stirring device is arranged on the kiln car), conveying the fine powder into a shuttle kiln, closing a kiln door, stirring at 550-650 ℃, and blowing oxygen for 2 hours;|[0054] (5) and (3) green compact forming and drying: uniformly mixing the decarburized fine powder and light-burned magnesium powder (the content of magnesium oxide is 97.8%) according to the weight ratio of 1: 2, and performing green pressing, forming and drying;|[0055] (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 7 hours at 3000 ℃;|[0056] (5) cooling, crushing and sorting the product.|[0057] The results are shown in Table 2. The prepared magnesia is further pressed into the lining brick of the ladle furnace, and after three ladle experiments in a Tangshan stainless steel factory, the lining brick of the ladle furnace has no obvious difference in use compared with the lining brick of the ladle furnace made of common fused magnesia.|[0058] TABLE 2|Example 1Example 2Example 3 SiO2 % 1.2 1.20 1.25 Al2O3 % 0.21 0.30 0.30 Fe2O3 % 0.98 1.00 0.95 CaO % 0.96 1.10 1.05 MgO % 96.12 96.20 96.20 IL 0.07 0.12 0.10 B.D 3.45 3.47 3.48 (CN101837996)|TECHNICAL FIELD|[0002] The invention relates to a preparation method of magnesia, in particular to a method for melting and purifying magnesia by using waste magnesium products.|BACKGROUND ART|[0004] The basic refractory material is a necessary product in industries such as steel, cement and the like, the main raw material of the basic refractory material is magnesia, although the magnesium ore resource in China is rich, the basic refractory material is a resource mineral product, and one part is less when being exploited, so the use of the basic refractory material needs to be reasonably planned. However, at present, the use of the alkaline refractory materials is basically disposable, the waste magnesia carbon bricks, magnesia bricks and the like are basically treated as garbage, and although the waste magnesia carbon bricks are also recycled at present, the recycled waste magnesia carbon bricks are used as waste materials and cannot be used for producing high-grade magnesia products, so that the waste of mineral resources is caused.|[0005] China is a large industrial country, a large iron and steel country, and more than ten million waste magnesia carbon bricks, the recycling of waste magnesia carbon bricks is struggled, and magnesia is a mineral resource and cannot be regenerated, so that the full utilization of waste magnesium products is imperative from the strategic point of long-term development.|DISCLOSURE|[0006] Disclosure of Invention|[0007] In order to solve the problems, the invention provides a method for melting and purifying magnesia by fully utilizing waste magnesium products, which not only saves resources, but also protects the environment.|[0008] In order to achieve the purpose, the invention adopts the technical scheme that: a method for melting and purifying magnesia by using waste magnesium products comprises the following steps:|[0009] (1) selecting raw materials: manually selecting various purchased waste magnesium products to remove macroscopic impurities;|[0010] generally, the main raw materials of waste magnesium products purchased are: used waste magnesia carbon bricks, magnesia bricks or expired and failed products of magnesia product manufacturers and the like.|[0011] The magnesia carbon brick and the magnesia brick are used, and impurities such as aluminum, iron, calcium and the like which are different from the brick are obviously remained on the surfaces of the magnesia carbon brick and the magnesia brick, so that the impurities are firstly removed manually when raw materials are selected, the high-temperature melting time is shortened, and the production cost is reduced.|[0012] (2) Crushing and deironing: crushing and finely grinding the waste magnesium products after the impurities are removed into fine powder below 800 meshes, and removing iron by using iron removal equipment;|[0013] (3) flotation and carbon removal: removing carbon from the iron-removed fine powder by a water flotation method;|[0014] (4) medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car, feeding the fine powder into a tunnel kiln or a shuttle kiln, closing a kiln door, stirring at 550-650 ℃, and blowing in oxygen for 2-4 hours;|[0015] (5) and (3) green compact forming and drying: uniformly mixing the fine powder subjected to carbon removal and light-burned magnesium powder according to the weight ratio of 1: 2-4, and performing green pressing and forming and drying;|[0016] (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 6-8 hours at 2500-3500 ℃;|[0017] (7) and cooling, crushing and sorting the product.|[0018] In the invention, impurities in waste magnesium products such as phosphate, resin and the like can be decomposed and volatilized in a high-temperature melting state, and the impurity which is least easy to remove is carbon.|[0019] The physical and chemical indexes of the magnesite prepared by the method are shown in Table 1.|[0020] TABLE 1|Index (I)97 electric smelting magnesiteMagnesite prepared by the method of the invention SiO2 % 1.13 ≤1.25 Al2O3 % 0.10 ≤0.3 Fe2O3 % 0.80 ≤1.0 CaO % 1.08 ≤1.2 MgO % 96.81 ≥96 IL 0.08 ≤0.12 B.D 3.48 ≤3.49 |[0022] It can be seen from table 1 that the magnesite prepared by the method of the present invention has a slightly lower purity than normal fused magnesite, but does not affect the use of magnesite because the content of alumina in the magnesite is higher. The method mainly depends on raw materials, recycled waste magnesia carbon bricks often contain metallic aluminum additives, and part of magnesia carbon bricks are likely to be mixed in the raw materials, so that the aluminum content of products is higher, the quality of magnesia sand is not influenced when alumina and magnesia are used for producing magnesia-alumina spinel in a high-temperature molten state, and the magnesia sand of the products is mainly used in the following aspects: the production of metallurgical refractory materials such as magnesia carbon bricks, magnesia alumina carbon bricks, magnesia bricks, ladle castable, tundish coating materials, electric furnace bottom ramming materials and the like has good effect, low production cost and cyclic utilization of resources, and accords with the national conditions of China. The magnesite prepared by the method is pressed into the lining brick of the ladle furnace, and after three ladle experiments in Tangshan stainless steel factories, the lining brick has no obvious difference in use compared with the lining brick of the ladle furnace prepared by common fused magnesite.|[0023] The invention has the beneficial effects that: saving resources and protecting environment. The invention makes full use of various waste magnesium products, such as waste magnesia carbon bricks, magnesia bricks or expired spent products of magnesium product manufacturers, and recycles the existing magnesia to the maximum extent. And secondly, energy is saved. Most of macroscopic impurities are removed through manual selection, and the high-temperature melting time is shortened. Secondly, the melting time of the electric arc furnace is directly influenced by the decarburization rate, namely the cost, and the direct hook is economical.|INVENTION MODE|[0024] Detailed Description|[0025] Example 1 method for purifying magnesite by melting waste magnesia carbon bricks|[0026] The method comprises the following steps:|[0027] (1) selecting raw materials: manually selecting and removing impurities such as aluminum, iron, calcium and the like which can be seen by naked eyes from purchased waste magnesia carbon bricks;|[0028] (2) crushing and deironing: crushing and finely grinding the waste magnesia carbon bricks after the impurities are removed into fine powder below 800 meshes, and removing iron by iron removal equipment;|[0029] (3) flotation and carbon removal: and (3) placing the fine powder subjected to iron removal in a water tank, and removing carbon by a water floatation method. The carbon floats on the water surface and the magnesia sinks at the water bottom by utilizing the different specific gravity of the carbon and the magnesia, so that most of the carbon is removed;|[0030] the carbon content of the fine powder after water flotation is 5 percent by measuring the total carbon content by adopting a combustion gravimetric method (the execution standard is GB/T13245-91).|[0031] (4) Medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car (a raw material stirring device is arranged on the kiln car), feeding the fine powder into a tunnel kiln, closing a kiln door, stirring at 550-650 ℃, and blowing oxygen for 3 hours;|[0032] (5) and (3) green compact forming and drying: uniformly mixing the decarburized fine powder and light-burned magnesium powder (the content of magnesium oxide is 97%) according to the weight ratio of 1: 3, and performing green pressing, forming and drying;|[0033] (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 7 hours at 3000 ℃;|[0034] (5) cooling, crushing and sorting the product.|[0035] The results are shown in Table 2. The prepared magnesia is further pressed into the lining brick of the ladle furnace, and after three ladle experiments in a Tangshan stainless steel factory, the lining brick of the ladle furnace has no obvious difference in use compared with the lining brick of the ladle furnace made of common fused magnesia.|[0036] Example 2 method for melting and purifying magnesite by using waste magnesite bricks|[0037] The method comprises the following steps:|[0038] (1) selecting raw materials: manually selecting and removing impurities such as aluminum, iron, calcium and the like which can be seen by naked eyes from purchased waste magnesia bricks;|[0039] (2) crushing and deironing: crushing and finely grinding the waste magnesia bricks after the impurities are removed into fine powder below 800 meshes, and removing iron by using iron removal equipment;|[0040] (3) flotation and carbon removal: and (3) placing the fine powder subjected to iron removal in a water tank, and removing carbon by a water floatation method.|[0041] The carbon content of the fine powder after flotation was 5% as determined by gravimetric combustion determination (the standard being applied is GB/T13245-91).|[0042] (4) Medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car (a raw material stirring device is arranged on the kiln car), conveying the fine powder into a shuttle kiln, closing a kiln door, stirring at 550-650 ℃, and blowing oxygen for 4 hours;|[0043] (5) and (3) green compact forming and drying: uniformly mixing the decarburized fine powder and light-burned magnesium powder (the content of magnesium oxide is 97.5%) according to the weight ratio of 1: 4, and performing green pressing, forming and drying;|[0044] (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 7 hours at 3000 ℃;|[0045] (5) cooling, crushing and sorting the product.|[0046] The results are shown in Table 2. The prepared magnesia is further pressed into the lining brick of the ladle furnace, and after three ladle experiments in a Tangshan stainless steel factory, the lining brick of the ladle furnace has no obvious difference in use compared with the lining brick of the ladle furnace made of common fused magnesia.|[0047] Example 3 method for melting and purifying magnesite by using waste magnesium product|[0048] The method comprises the following steps:|[0049] (1) selecting raw materials: manually selecting expired and failed magnesium products of purchased waste magnesium product manufacturers to remove macroscopic impurities;|[0050] (2) crushing and deironing: crushing and finely grinding the waste magnesium product after removing impurities into fine powder below 800 meshes, and removing iron by using iron removal equipment;|[0051] (3) flotation and carbon removal: and (3) placing the fine powder subjected to iron removal in a water tank, and removing carbon by a water floatation method.|[0052] The carbon content of the fine powder after flotation was 5% as determined by gravimetric combustion determination (the standard being applied is GB/T13245-91).|[0053] (4) Medium-temperature carbon removal: loading the fine powder subjected to flotation and carbon removal into a kiln car (a raw material stirring device is arranged on the kiln car), conveying the fine powder into a shuttle kiln, closing a kiln door, stirring at 550-650 ℃, and blowing oxygen for 2 hours;|[0054] (5) and (3) green compact forming and drying: uniformly mixing the decarburized fine powder and light-burned magnesium powder (the content of magnesium oxide is 97.8%) according to the weight ratio of 1: 2, and performing green pressing, forming and drying;|[0055] (6) melting and crystallizing: feeding the dried blank into a high-temperature electric arc furnace, and melting for 7 hours at 3000 ℃;|[0056] (5) cooling, crushing and sorting the product.|[0057] The results are shown in Table 2. The prepared magnesia is further pressed into the lining brick of the ladle furnace, and after three ladle experiments in a Tangshan stainless steel factory, the lining brick of the ladle furnace has no obvious difference in use compared with the lining brick of the ladle furnace made of common fused magnesia.|[0058] TABLE 2|Example 1Example 2Example 3 SiO2 % 1.2 1.20 1.25 Al2O3 % 0.21 0.30 0.30 Fe2O3 % 0.98 1.00 0.95 CaO % 0.96 1.10 1.05 MgO % 96.12 96.20 96.20 IL 0.07 0.12 0.10 B.D 3.45 3.47 3.48 Family Number|(7093988)|7093988|Abstract|(CN101837996B B)|The invention relates to a method for the melting purification of magnesia by using a waste magnesium product . The adopted technical scheme is that the method comprises the following steps of : manually picking out and removing impurities visible to the naked eye from various purchased waste magnesium products ; crushing and grinding the waste magnesium products subjected to the impurity removal into powder of below 800 meshes and removing iron with an iron removing device ; removing carbon from the powder subjected to the iron removal by the water floatation method ; loading the powder subjectedto the carbon removal by the water floatation method into a kiln bogie , conveying the kiln bogie loaded with the powder to a tunnel kiln or a shuttle kiln , closing the kiln door , stirring the powder at the temperature of 550 to 650 DEG C and blowing in oxygen for 2 to 4 hours ; uniformly mixing the powder subjected to the carbon removal with light burnt magnesium powder in a weight ratio of 1 : 2-4 and performing compression molding and drying ; conveying the dried blank to a high - temperature electric arc furnace for melting at the temperature of 2,500 to 3,500 DEG C for 6 to 8 hours ; and cooling , crushing and selecting the products . The method has the advantages of saving resource , protecting environment and saving energy . |IPC codes|(CN101837996B B)|C01F - 005/02 | Materials, metallurgy Y02P-020/10 Y02P-020/10 C01F-005/02 C01F-005/02 CN114163218|CN106179769|CN103819179|CN115819073B|CN104550187B CN114163218 99063572 WHO=Examiner SELF=N CAT=Y|CN106179769 74824729 WHO=Examiner SELF=N CAT=A|CN103819179 66107215 WHO=Examiner SELF=N CAT=A|CN115819073B 104162023 WHO=Examiner SELF=N|CN104550187B 69210546 WHO=Examiner SELF=N CN101565280|CN101480564|CN1150131|DD-232904 CN101565280 62176526 WHO=Examiner SELF=N|CN101480564 6793670 WHO=Examiner SELF=N|CN1150131 4790202 WHO=Examiner SELF=N|DD-232904 10290747 WHO=Examiner SELF=N 《耐火材料》 20050822 田守信等 用后镁碳砖的再生研究 第39卷, 第04期 2 CN101480564; CN101565280; CN1150131; DD-232904 LAPSED (CN101837996)|LAPSED DEAD (CN101837996)|DEAD (CN101837996)|LEGAL DETAILS FOR CN101837996|Actual or expected expiration date=2014-07-16|Legal state=DEAD|Status=LAPSED|Event publication date=2010-05-25|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201010181711|Application date=2010-05-25|Standardized application number=2010CN-0181711|Event publication date=2010-09-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN101837996|Publication stage code=A|Publication date=2010-09-22|Standardized publication number=CN101837996|Event publication date=2010-09-22|Event code=CN/C06|Event indicator=Pos|Event group=Examination events|Publication|Event publication date=2010-11-10|Event code=CN/C10|Event group=Examination events|Request of examination as to substance|Event publication date=2011-09-21|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN101837996|Publication stage code=B|Publication date=2011-09-21|Standardized publication number=CN101837996B|Event publication date=2011-09-21|Event code=CN/C14|Event indicator=Pos|Event group=Event indicating In Force|Granted|Event publication date=2014-07-16|Event code=CN/C17|Event indicator=Neg|Event group=Event indicating Not In Force|Cessation of Patent Right https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjmpfwjuNfED0hj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=9Ped%252Bc2GOTDJjVi4WaO%252BSrmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN101837996)|NAME=JIN CHUNHUA;SHENYANG JACK INTELLECTUAL PROPERTY AGENT LTD.|(CN101837996)|NAME=JIN CHUNHUA;SHENYANG JACK INTELLECTUAL PROPERTY AGENT LTD. (CN101837996)|NAME=WANG XI|NAME=ZHU YONGZHENG|(CN101837996)|NAME=WANG XI|NAME=ZHU YONGZHENG 0 1 Titre: (CN101837996)|Method for melting purification of magnesia by using waste magnesium product Résumé: (CN101837996)|The invention relates to a method for the melting purification of magnesia by using a waste magnesium product. The adopted technical scheme is that the method comprises the following steps of: manually picking out and removing impurities visible to the naked eye from various purchased waste magnesium products; crushing and grinding the waste magnesium products subjected to the impurity removal into powder of below 800 meshes and removing iron with an iron removing device; removing carbon from the powder subjected to the iron removal by the water floatation method; loading the powder subjectedto the carbon removal by the water floatation method into a kiln bogie, conveying the kiln bogie loaded with the powder to a tunnel kiln or a shuttle kiln, closing the kiln door, stirring the powder at the temperature of 550 to 650 DEG C and blowing in oxygen for 2 to 4 hours; uniformly mixing the powder subjected to the carbon removal with light burnt magnesium powder in a weight ratio of 1:2-4 and performing compression molding and drying; conveying the dried blank to a high-temperature electric arc furnace for melting at the temperature of 2,500 to 3,500 DEG C for 6 to 8 hours; and cooling, crushing and selecting the products. The method has the advantages of saving resource, protecting environment and saving energy. 61 Abstract gpt-4o-mini no The article describes a method for purifying magnesia from waste magnesium products, which does not relate to accelerated weathering or CO₂ capture.
63 CN202311616678 CN202311616678 CN117585678|CN117585678 108619719 CN117585678 B 2024-08-27 [CN117585678B]|CN117585678 A 2024-02-23 [CN117585678] 2023-11-30 2023-11-30 2024-08-27|2024-02-23 (CN117585678B)|2024-08-27 (CN117585678)|2043-11-30 (CN117585678)|Nitrogen absorption treatment method for new thermal field for synthesizing silicon carbide powder by PVT furnace (CN117585678)|The invention discloses a nitrogen absorption treatment method for a new thermal field for synthesizing silicon carbide powder in a PVT furnace, and the treatment method comprises the following steps: a pretreatment step: carrying out high-temperature carbon removal on an adsorbent to obtain a pretreated adsorbent; a new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating and pressurizing, maintaining for a period of time, cooling, and taking out the adsorbent; the synthesis method comprises the following steps: uniformly mixing silicon powder and graphite powder, putting the mixture into a crucible of a new thermal field, carrying out a synthesis reaction of silicon carbide powder to obtain blocky silicon carbide, and crushing, grinding, screening, decarbonizing, cleaning and drying the silicon carbide to obtain the silicon carbide powder which can be used for silicon carbide single crystal growth. The adsorbent selected by the invention is silicon carbide, so that the economic cost is saved, and the nitrogen removal effect is good. NINGBO ALPHA SEMICONDUCTOR (CN117585678)|NINGBO HESHENG NEW MAT CO LTD ([CN])|(CN117585678)|NINGBO HESHENG NEW MAT CO LTD ([CN]) ZHANG WENZHONG|HAO HAN|ZHAO XINTIAN (CN117585678)|Zhang Wenzhong|Hao Han|Zhao Xintian|(CN117585678)|ZHANG WENZHONG|HAO HAN|ZHAO XINTIAN (CN117585678)|YUAN HONGBO;NINGBO YONGXIN HECHUANG INTELLECTUAL PROPERTY AGENCY CO., LTD|Reg. Nb: 33552 (CN117585678)|Therefore, there is a need for a nitrogen removal process for silicon carbide crystal growth materials that is economical, simple and easy to operate, reduces the nitrogen content in the silicon carbide growth materials, and improves the stability of the resistivity of subsequent silicon carbide crystals.| (CN117585678)|1. A nitrogen-absorbing treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace is characterized by comprising the following steps of,Pretreatment: carrying out high Wen Chutan on the adsorbent to obtain white or light green pretreated adsorbent; And (3) a new thermal field blank firing step: placing the crucible in a new thermal field, heating and pressurizing the new thermal field and the crucible for a period of time, and finally cooling the crucible and the new thermal field; the heating and pressurizing of the new thermal field blank burning step comprises two stages, wherein the temperature is raised to 1000-1200 ℃ in the first stage, the pressure in the first stage is set to be below 5x10 -5 mbar, and the maintaining time is 2-5 h; the second stage is to raise the temperature to 2000-2200 deg.c, maintain the pressure below 5x10 -3 mbar and maintain the pressure for 20-40 hr; A new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating, pressurizing and maintaining for a period of time, cooling, taking out the adsorbent, observing the color of the adsorbent, and repeating the pretreatment step and the new thermal field nitrogen absorption step for a plurality of times if the adsorbent is dark green until the color of the adsorbent is light green; the temperature of the new thermal field nitrogen absorbing step is set to 2000-2200 ℃, the pressure is set to 100-500 mbar, and the heat preservation time is 20-40 h; The synthesis steps are as follows: uniformly mixing silicon powder and graphite powder, placing the mixture in a crucible of a new thermal field to perform a synthesis reaction of silicon carbide powder to obtain massive silicon carbide, crushing, grinding, screening, decarbonizing, cleaning and drying the silicon carbide to obtain the silicon carbide powder which can be used for silicon carbide single crystal growth; the adsorbent is silicon carbide. | (CN117585678)|As another preferable aspect, the adsorbent is 80 to 300 mesh silicon carbide powder.|The application discloses a nitrogen absorption treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace, which comprises the following steps of: carrying out high Wen Chutan on the adsorbent to obtain a pretreated adsorbent; a new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating, pressurizing and maintaining for a period of time, cooling and taking out the adsorbent; the synthesis steps are as follows: the silicon powder and the graphite powder are uniformly mixed, and the mixture is placed in a crucible of a new thermal field to carry out the synthesis reaction of the silicon carbide powder to obtain massive silicon carbide, and the silicon carbide is crushed, ground, screened, decarbonized, cleaned and dried to obtain the silicon carbide powder which can be used for the growth of silicon carbide single crystals.|The application relates to the technical field of silicon carbide synthesis, in particular to a nitrogen absorption treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace.| (CN117585678)|SILICON CARBIDE(100,156)|PVT FURNACE(100,16)|SYNTHESIZING SILICON CARBIDE(100,11)|NITROGEN ABSORBING TREATMENT(100,9)|NITROGEN ABSORPTION TREATMENT(100,6)|PRETREATED ADSORBENT(96,10)|ADSORBENT(57,46)|PVT FURNACE SYNTHESIS(56,2)|GRAPHITE POWDER(47,8)|ADSORBENT COLOR(47,6)|NITROGEN ABSORPTION(41,15)|MASSIVE SILICON CARBIDE(40,11)|CRUCIBLE(38,40)|BLANK BURNING(36,2)|LIGHT GREEN PRETREATED ADSORBENT(36,1)|SILICON POWDER(35,9)|PVT FURNACE SYNTHETIC(35,1)|SILICON CARBIDE POWDER(34,75)|ADSORBENT PURITY(33,1)|WEN(31,4)|PRETREATMENT(30,22)|PRESSURIZING(29,5)|SILICON CARBIDE SYNTHESIS(27,1)|MESH SILICON CARBIDE(25,12)|NITROGEN CONTENT(20,16)|DECARBONIZATION(20,4)|MBAR(19,7)|SILICON CARBIDE CRYSTAL(19,2)|SILICON CARBIDE CRYSTAL GROWTH(19,1)|THERMAL FIELD CRUCIBLE(18,6)|SILICON CARBIDE SYNTHESIS REACTION(17,5)|SYNTHESIS REACTION(16,8)|CRUSHING(16,5)|GETTERING TREATMENT(16,2)|FIRE(15,12)|GRINDING(14,4)|REMOVING NITROGEN(14,3)|SYNTHESIZING(14,3)|SCREENING(13,6)|CRYSTAL GROWTH(13,1)|QUARTZ TUBE FURNACE(12,4)|SILICON CARBIDE GROWTH MATERIAL(11,1)|DARK GREEN(10,8)|LIGHT GREEN(10,6)|SILICON CARBIDE SINGLE CRYSTAL(10,3)|GROWTH MATERIAL(10,1)|NITROGEN REMOVAL(10,1)|AIR INTRODUCTION(9,4)|ADSORBENT SILICON CARBIDE(8,3)|NITROGEN GETTERING(8,3)|SILICON CARBON MOLAR RATIO(8,3)|HEAT PRESERVATION TIME(7,3)|CONFLICT PREMISE(7,1)|GRAPHITE INSULATION FELT(7,1)|PRETREATED ADSORBENT COLOR(7,1)|SINGLE CRYSTAL(6,7)|SINGLE CRYSTAL GROWTH(6,5)|ECONOMIC COST(6,3)|GREEN COLOR(6,2)|ADSORBENT ADSORPTION(6,1)|DARK GREENISH BLACK(6,1)|NITROGEN ABSORBING TREATMENT(6,1)|NONEXCLUSIVE INCLUSION(6,1)|UNQUALIFIED RESISTIVITY(6,1)|AVERAGE PARTICLE DIAMETER(5,2)|CRUCIBLE COVER(5,2)|GROWING SILICON CARBIDE(5,2)|MAINTENANCE TIME(5,2)|SILICON CARBIDE POWDER SYNTHESIS(5,2)|GRAPHITE HEAT PRESERVATION FELT(5,1)|GRAPHITE SOFT FELT(5,1)|INSULATING CRUCIBLE(5,1)|PARTICLE CRYSTALLINITY(5,1)|DIGITAL PHOTOGRAPH(4,6)|CARBON POWDER(4,2)|CRYSTAL PRODUCTION(4,2)|PVT(4,2)|ADSORBENT NITROGEN ABSORBING CAPACITY(4,1)|ADSORBENT NITROGEN CONTENT(4,1)|EMPTY BURNING(4,1)|NITROGEN ADSORPTION TREATMENT(4,1)|PERIPHERAL HEAT PRESERVATION FELT(4,1)|PURITY ARGON(4,1)|PURITY NITROGEN CONTENT(4,1)|SILICON CARBIDE AGGLOMERATE(4,1)|SIC(3,4)|ARGON INTRODUCTION(3,1)|CIRCUMFERENTIAL ARRAY(3,1)|ENERGY AUTOMOBILE(3,1)|GRAPHITE PIECE(3,1)|PERIPHERAL ISOLATION(3,1)|SATURATED ELECTRON MOBILITY(3,1)||(CN117585678)|SILICON CARBIDE(100,156)|PVT FURNACE(100,18)|NITROGEN ABSORBING TREATMENT(100,11)|SYNTHESIZING SILICON CARBIDE(100,11)|NITROGEN ABSORPTION TREATMENT(100,6)|PRETREATED ADSORBENT(82,10)|PVT FURNACE SYNTHESIS(47,2)|ADSORBENT(42,46)|GRAPHITE POWDER(40,8)|GRAPHITE SOFT FELT(39,1)|SILICON CARBIDE POWDER(35,76)|MASSIVE SILICON CARBIDE(34,11)|PVT FURNACE SYNTHETIC(30,1)|SILICON POWDER(29,9)|ADSORBENT PURITY(28,1)|CRUCIBLE(27,39)|NITROGEN ABSORPTION(27,14)|NITROGEN CONTENT(25,16)|PRESSURIZING(25,5)|WEN(24,5)|PRETREATMENT(23,22)|SILICON CARBIDE SYNTHESIS(23,1)|DECARBONIZATION(17,4)|MESH SILICON CARBIDE(16,13)|SILICON CARBIDE CRYSTAL(16,2)|SILICON CARBIDE CRYSTAL GROWTH(16,1)|THERMAL FIELD CRUCIBLE(15,6)|CRYSTAL PRODUCTION(15,2)|CRUSHING(14,5)|SILICON CARBIDE SYNTHESIS REACTION(14,5)|SYNTHESIS REACTION(13,8)|GRINDING(12,4)|REMOVING NITROGEN(12,3)|SCREENING(11,6)|SYNTHESIZING(11,3)|BLANK FIRING(11,1)|CRYSTAL GROWTH(11,1)|FIRE(10,12)|QUARTZ TUBE FURNACE(10,4)|SILICON CARBIDE SINGLE CRYSTAL(9,3)|GETTERING TREATMENT(9,1)|GROWTH MATERIAL(9,1)|NITROGEN REMOVAL(9,1)|SILICON CARBIDE GROWTH MATERIAL(9,1)|AIR INTRODUCTION(8,3)|NITROGEN ABSORBING TREATMENT(8,2)|ADSORBENT SILICON CARBIDE(7,3)|NITROGEN GETTERING(7,3)|SILICON CARBON MOLAR RATIO(7,2)|AVERAGE PARTICLE DIAMETER(6,4)|CONFLICT PREMISE(6,1)|GRAPHITE INSULATION FELT(6,1)|PRETREATED ADSORBENT COLOR(6,1)|SINGLE CRYSTAL(5,7)|SINGLE CRYSTAL GROWTH(5,5)|ECONOMIC COST(5,3)|GREEN COLOR(5,2)|ADSORBENT ADSORPTION(5,1)|DARK GREENISH BLACK(5,1)|NONEXCLUSIVE INCLUSION(5,1)|UNQUALIFIED RESISTIVITY(5,1)|DIGITAL PHOTOGRAPH(4,6)|CRUCIBLE COVER(4,2)|GROWING SILICON CARBIDE(4,2)|SILICON CARBIDE POWDER SYNTHESIS(4,2)|ADSORBENT NITROGEN ABSORBING CAPACITY(4,1)|BLANK BURNING(4,1)|EMPTY BURNING(4,1)|GRAPHITE HEAT PRESERVATION FELT(4,1)|INSULATING CRUCIBLE(4,1)|NITROGEN ADSORPTION TREATMENT(4,1)|PARTICLE CRYSTALLINITY(4,1)|PERIPHERAL HEAT PRESERVATION FELT(4,1)|PURITY ARGON(4,1)|PURITY NITROGEN CONTENT(4,1)|SILICON CARBIDE AGGLOMERATE(4,1)|THERMAL FIELD NITROGEN ABSORBING(4,1)|MBAR(3,5)|SIC(3,4)|CARBON POWDER(3,2)|PVT(3,2)|ARGON INTRODUCTION(3,1)|CIRCUMFERENTIAL ARRAY(3,1)|ENERGY AUTOMOBILE(3,1)|GRAPHITE PIECE(3,1)| (CN117585678)|1. A nitrogen-absorbing treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace is characterized by comprising the following steps of,|Pretreatment: carrying out high Wen Chutan on the adsorbent to obtain white or light green pretreated adsorbent;| And (3) a new thermal field blank firing step: placing the crucible in a new thermal field, heating and pressurizing the new thermal field and the crucible for a period of time, and finally cooling the crucible and the new thermal field; the heating and pressurizing of the new thermal field blank burning step comprises two stages, wherein the temperature is raised to 1000-1200 ℃ in the first stage, the pressure in the first stage is set to be below 5x10 -5 mbar, and the maintaining time is 2-5 h; the second stage is to raise the temperature to 2000-2200 deg.c, maintain the pressure below 5x10 -3 mbar and maintain the pressure for 20-40 hr; | A new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating, pressurizing and maintaining for a period of time, cooling, taking out the adsorbent, observing the color of the adsorbent, and repeating the pretreatment step and the new thermal field nitrogen absorption step for a plurality of times if the adsorbent is dark green until the color of the adsorbent is light green; the temperature of the new thermal field nitrogen absorbing step is set to 2000-2200 ℃, the pressure is set to 100-500 mbar, and the heat preservation time is 20-40 h; | The synthesis steps are as follows: uniformly mixing silicon powder and graphite powder, placing the mixture in a crucible of a new thermal field to perform a synthesis reaction of silicon carbide powder to obtain massive silicon carbide, crushing, grinding, screening, decarbonizing, cleaning and drying the silicon carbide to obtain the silicon carbide powder which can be used for silicon carbide single crystal growth; | the adsorbent is silicon carbide. |2. A new thermal field nitrogen-absorbing treatment process for synthesizing silicon carbide powder in a PVT furnace as described in claim 1, wherein said adsorbent is 40-300 mesh silicon carbide powder.|3. A new thermal field nitrogen-absorbing treatment method for synthesizing silicon carbide powder in a PVT furnace as described in claim 2, wherein said adsorbent is 80-300 mesh silicon carbide powder.|4. A new thermal field nitrogen-gettering treatment process for PVT furnace synthesis of silicon carbide powder as described in claim 2 wherein said adsorbent is the product of said synthesis step.|5. A new thermal field nitrogen-gettering treatment process for PVT furnace synthesis of silicon carbide powder as described in claim 1 wherein said adsorbent has a nitrogen content of less than 5*e 16 at/cm3.|6. The nitrogen-absorbing treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace according to claim 1, wherein the purity of the adsorbent is 99.9999% or more.|7. The nitrogen-absorbing treatment method for a new thermal field of PVT furnace synthetic silicon carbide powder according to claim 1, wherein the pretreatment step specifically comprises: and placing the adsorbent in a quartz tube furnace, introducing air into the furnace, heating to 900-1000 ℃, and keeping the temperature for 6-8 hours.|8. The nitrogen-absorbing treatment method for a new thermal field for synthesizing silicon carbide powder in a PVT furnace according to claim 1, wherein the synthesizing step specifically comprises: the silicon powder and the graphite powder are mixed according to the silicon-carbon molar ratio of (1-1.1): 1 are evenly mixed and placed in a crucible of a new thermal field, the temperature is 2000-2200 ℃, the pressure is 0-800 mbar, the reaction time is 20-50 h, and the synthesis reaction of silicon carbide is carried out, thus obtaining the massive silicon carbide. (CN117585678)|TECHNICAL FIELD|Technical Field|[0001] The application relates to the technical field of silicon carbide synthesis, in particular to a nitrogen absorption treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace.|BACKGROUND ART|[0002] Silicon carbide (SiC) is a popular material for third generation semiconductors, and is widely used in industries such as 5G communication, new energy automobiles, photovoltaic inverters, and the like, due to its excellent characteristics of wide forbidden band, high saturated electron mobility, high breakdown electric field, high thermal conductivity, and the like.|[0003] The synthesis method of the high-purity silicon carbide powder used for the growth of the third-generation semiconductor silicon carbide single crystal comprises the following steps: liquid phase, solid phase and gas phase processes. The solid phase method (improving the self-propagating method to synthesize the silicon carbide is also called PVT method) is used for preparing the high-purity silicon carbide, and has the characteristics of high purity, high yield, good particle crystallinity and the like, and is widely popularized.|[0004] The growth raw materials of the silicon carbide crystal are that after the high-purity silicon powder and carbon powder are uniformly mixed, the mixture is filled into a graphite crucible, then the crucible is filled into a new thermal field, the new thermal field is put into a PVT furnace and heated to 2000-2200 ℃ to react and synthesize high-purity silicon carbide blocks, and finally the silicon carbide powder with the required mesh number is prepared through the procedures of crushing, grinding, screening, decarbonizing, cleaning, drying and the like.|[0005] When the PVT method is adopted to grow the silicon carbide powder, the novel heat-insulating material adsorbs a large amount of nitrogen in the preparation process, and when the silicon carbide powder is synthesized at a high temperature, the materials release the nitrogen adsorbed in the interior, so that the nitrogen content in the grown silicon carbide powder is higher. The silicon carbide powder adsorbs excessive nitrogen, and the color of the silicon carbide powder is black or dark greenish black, so that the silicon carbide powder cannot be used for synthesizing silicon carbide single crystal growth.|[0006] Silicon carbide powder for silicon carbide single crystal growth requires low metal and nitrogen content, and has extremely high nitrogen content, and the excessive nitrogen content can cause unqualified resistivity of the silicon carbide single crystal to be grown and discharged, so that economic loss is caused. Therefore, there is a need for a nitrogen removal process for silicon carbide crystal growth materials that is economical, simple and easy to operate, reduces the nitrogen content in the silicon carbide growth materials, and improves the stability of the resistivity of subsequent silicon carbide crystals.|DISCLOSURE|Disclosure of Invention|[0007] The application aims to reduce the nitrogen content in the new thermal field graphite soft felt, so that the nitrogen content in the silicon carbide powder synthesized by a PVT furnace can meet the requirement of crystal production.|[0008] In order to achieve the above purpose, the application adopts the following technical scheme: a nitrogen-absorbing treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace comprises the following steps of: carrying out high Wen Chutan on the adsorbent to obtain a pretreated adsorbent; a new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating, pressurizing and maintaining for a period of time, cooling and taking out the adsorbent; the synthesis steps are as follows: uniformly mixing silicon powder and graphite powder, placing the mixture in a crucible of a new thermal field to perform a synthesis reaction of silicon carbide powder to obtain massive silicon carbide, crushing, grinding, screening, decarbonizing, cleaning and drying the silicon carbide to obtain the silicon carbide powder which can be used for silicon carbide single crystal growth; the adsorbent is silicon carbide.|[0009] Preferably, the adsorbent is 40 to 300 mesh silicon carbide powder.|[0010] As another preferable aspect, the adsorbent is 80 to 300 mesh silicon carbide powder.|[0011] As another preference, the adsorbent is the product of the synthesis step.|[0012] As another preference, the nitrogen content of the adsorbent is less than 5*e 16 at/cm3.|[0013] As another preferable aspect, the adsorbent has a purity of 99.9999% or more.|[0014] As another preferable mode, the temperature of the new thermal field nitrogen absorbing step is set to 2000-2200 ℃, the pressure is 100-500 mbar, and the heat preservation time is 20-40 h.|[0015] As another preferable, the pretreatment step specifically includes: and placing the adsorbent in a quartz tube furnace, introducing air into the furnace, heating to 900-1000 ℃, and keeping the temperature for 6-8 hours.|[0016] As another preferable mode, the synthesizing step specifically includes: the silicon powder and the graphite powder are mixed according to the silicon-carbon molar ratio of (1-1.1): 1 are evenly mixed and placed in a crucible of a new thermal field, the temperature is 2000-2200 ℃, the pressure is 0-800 mbar, the reaction time is 20-50 h, and the synthesis reaction of silicon carbide is carried out, thus obtaining the massive silicon carbide.|[0017] As another preferable mode, the method further comprises a new thermal field blank firing step after the pretreatment step, wherein the new thermal field blank firing step specifically comprises the following steps: placing the crucible in a new thermal field, heating and pressurizing the new thermal field and the crucible for a period of time, and finally cooling the crucible and the new thermal field.|[0018] Compared with the prior art, the application has the beneficial effects that:|[0019] (1) According to the application, 40-300 meshes of silicon carbide powder is used as an adsorbent, and Si and SiC 2 components are evaporated through the silicon carbide powder, so that nitrogen in the device can be well adsorbed, and the nitrogen content in the silicon carbide powder is reduced; |[0020] (2) The application adopts the silicon carbide powder as the adsorbent, can simply judge the adsorption effect by observing the color of the adsorbent, and the silicon carbide powder with 40-300 meshes is waste material after the synthesis step, so that the adsorbent is not required to be purchased additionally, and the economic cost is saved. |DRAWINGS DESCRIPTION|[0021] FIG. 1 is a schematic view of an apparatus for manufacturing silicon carbide powder according to an embodiment of the present application;|[0022] FIG. 2 is a digital photograph of the adsorbent silicon carbide after the pretreatment step of example 1 of the present application; |[0023] FIG. 3 is a digital photograph of the adsorbent silicon carbide after the first new thermal field nitrogen gettering step of example 2 of the present application; |[0024] FIG. 4 is a digital photograph of the adsorbent silicon carbide after the second new thermal field nitrogen gettering step of example 2 of the present application; |[0025] FIG. 5 is a digital photograph of silicon carbide powder prepared in example 1 of the present application; |[0026] FIG. 6 is a digital photograph of silicon carbide powder prepared in example 2 of the present application; |[0027] FIG. 7 is a digital photograph of silicon carbide powder prepared in comparative example 1 of the present application; |[0028] in the figure: 1. a crucible; 2. a crucible cover; 21. a through hole; 3. a graphite heating cylinder; 4. graphite insulation felt; 41. a thermal insulation felt is arranged on the upper surface; 42. and a peripheral heat insulation felt. |INVENTION MODE|Detailed Description|[0029] The present application will be further described with reference to the following specific embodiments, and it should be noted that, on the premise of no conflict, new embodiments may be formed by any combination of the embodiments or technical features described below.|[0030] The terms "comprises" and "comprising," along with any variations thereof, in the description and claims, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.|[0031] The application provides a nitrogen-absorbing treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace, which comprises a pretreatment step, a new thermal field nitrogen-absorbing step and a synthesis step.|[0032] Pretreatment: carrying out high Wen Chutan on the adsorbent to obtain a pretreated adsorbent;|[0033] A new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating, pressurizing and maintaining for a period of time, cooling and taking out the adsorbent; |[0034] The synthesis steps are as follows: and (3) uniformly mixing the silicon powder and the graphite powder, placing the mixture into a crucible of a new thermal field to perform a synthesis reaction of silicon carbide powder to obtain massive silicon carbide, and then crushing, grinding, screening, decarbonizing, cleaning and drying the massive silicon carbide to obtain the silicon carbide powder which can be used as a growth raw material for growing silicon carbide single crystals. |[0035] In some embodiments, the adsorbent is 40-300 mesh silicon carbide powder. The adsorbent is silicon carbide powder, si and SiC 2 components are evaporated from the silicon carbide powder at high temperature, and simultaneously nitrogen is slowly released from growth equipment, graphite pieces and heat insulation materials in a high-temperature environment, and the released nitrogen is captured by Si and SiC 2 steam, so that the nitrogen is adsorbed in a new thermal field nitrogen adsorption step.|[0036] The silicon carbide powder with 40-300 meshes is used as the adsorbent, the specific surface area of the powder is large, the nitrogen content is low, and the rest silicon carbide powder except for sublimation of the silicon carbide powder can also play a role in adsorption.|[0037] In addition, the adsorbent is silicon carbide powder with 40-300 meshes, so that waste materials in the production link can be utilized, the adsorbent is not required to be purchased additionally, and the economic cost can be saved. After the synthesis of the synthesis step is finished, crushing massive silicon carbide, grinding the massive silicon carbide into particles, and sieving the particles to obtain 8-40-mesh silicon carbide powder serving as a growth raw material for growing silicon carbide single crystals, wherein the rest 40-mesh silicon carbide powder can be used as an adsorbent in the pretreatment step after sieving, so that the raw material is saved, and the method is economical and environment-friendly.|[0038] In some preferred embodiments, after the new thermal field nitrogen absorption step is completed, the color of the adsorbent is observed, and if the adsorbent is dark green, the pretreatment step and the new thermal field nitrogen absorption step may be repeated multiple times until the adsorbent color is light green, indicating that most of the nitrogen in the new thermal field is removed, and the synthesis step may be performed.|[0039] The adsorbent uses silicon carbide powder, the color of the 40-300 mesh silicon carbide powder obtained by screening is black, and the color of the silicon carbide powder becomes white after the pretreatment step is carried out, and the height of the silicon carbide powder is Wen Chutan. After the silicon carbide powder adsorbs nitrogen, the color is changed from white to dark green or even black, so that the silicon carbide powder is used as the adsorbent, and whether the nitrogen in the device is reduced to a state capable of synthesizing the universal crystal raw material can be judged through the color change of the adsorbent after the new thermal field nitrogen adsorption step. That is, the color of the adsorbent is observed after the new thermal field nitrogen adsorption step, if the adsorbent still presents dark green, the nitrogen in the device is not completely adsorbed and removed, and the pretreatment step and the new thermal field nitrogen adsorption step can be repeated until the adsorbed adsorbent presents light green, and the nitrogen in the device is completely removed.|[0040] The application uses silicon carbide powder as the adsorbent, has better nitrogen adsorption effect, and can simply judge the nitrogen removal effect in the silicon carbide powder synthesis device through the color change of the adsorbent, thereby ensuring that the synthesized silicon carbide powder with high purity is used as the growth raw material of silicon carbide single crystals.|[0041] In some embodiments, the adsorbent is 40-300 mesh (national standard) silicon carbide powder having a purity of 99.9999% or greater.|[0042] In some embodiments, the adsorbent is 40-300 mesh (national standard) silicon carbide powder having a nitrogen content of less than 5*e 16at/cm3.|[0043] In some preferred embodiments, the adsorbent is 80-300 mesh silicon carbide powder, with better adsorption.|[0044] In some embodiments, the temperature of the new thermal field nitrogen absorption step is set to 2000-2200 ℃, the pressure is set to 100-500 mbar, and the heat preservation time is 20-40 h.|[0045] In some embodiments, the method of manufacturing silicon carbide powder further comprises a new thermal field blank firing step disposed after the pretreatment step and before the new thermal field nitrogen gettering step.|[0046] And (3) a new thermal field blank firing step: placing the crucible in a new thermal field, heating and pressurizing the crucible in the new thermal field for a period of time, and finally cooling the crucible and the new thermal field.|[0047] In some embodiments, the new thermal field blank firing step uses the new thermal field to heat and pressurize the crucible in two stages of heat and pressure. Heating to 1000-1200 deg.c in the first stage with pressure below 5x 10 -5 mbar and maintaining for 2-5 hr; in the second stage, the temperature is raised to 2000-2200 ℃, the pressure is maintained below 5x 10 -3 mbar, the maintaining time is 20-40 h, and finally the new thermal field and the crucible are cooled.|[0048] The empty burning step mainly aims at utilizing negative pressure and high temperature to discharge nitrogen adsorbed in the new thermal field material through heating and pressurizing, so that the nitrogen in the new thermal field is primarily removed, and the using amount of the adsorbent in the later stage is saved.|[0049] In some embodiments, the pretreatment step comprises placing the adsorbent in a quartz tube furnace, introducing air into the tube furnace, heating to 900-1000 ℃, and maintaining the temperature for 6-8 hours to obtain the pretreated adsorbent, wherein the color of the pretreated adsorbent is white.|[0050] In some embodiments, the synthesis step comprises mixing silicon powder and graphite powder in a molar ratio of Si to C of (1 to 1.1): 1, uniformly mixing, placing the mixture into a crucible of a new thermal field to perform a synthesis reaction of silicon carbide powder, wherein the temperature is 2000-2200 ℃, and filling inert gas into a reaction device to control the pressure to be 0-800 mbar, wherein the synthesis reaction time is 20-50 h, so as to obtain silicon carbide agglomerates.|[0051] In some preferred embodiments, the median particle diameter D50 of the silicon powder is 0.3-3 mm, and the purity is greater than or equal to 99.9999%; the median particle diameter D50 of the graphite powder is 20-200 mu m, and the purity is more than or equal to 99.9999%.|[0052] In some embodiments, the inert gas in the synthesis step is high purity argon having a nitrogen content of less than 5 x 10 -3 ppm and a purity of 99.9999% or greater.|[0053] As shown in FIG. 1, the application also provides a silicon carbide powder synthesizing device for silicon carbide single crystal growth, which comprises a crucible 1 and a crucible cover 2 above the crucible 1, wherein a graphite heating cylinder 3 for heating is arranged outside the crucible 1, and a graphite heat preservation felt 4 for heat preservation is arranged outside the graphite heating cylinder 3.|[0054] The graphite heating cylinder 3 is tightly attached to the outer wall and the bottom of the crucible 1, so that the graphite heating cylinder 3 can rapidly transfer heat to the crucible 1, and heat loss is reduced. The graphite heat preservation felt 4 comprises an upper heat preservation felt 41 and a peripheral heat preservation felt 42, wherein the peripheral heat preservation felt 42 is arranged on the outer side of the graphite heating cylinder 3 in a surrounding mode, heat preservation is conducted on the outer side of the graphite heating cylinder 3, temperature loss is avoided, heat is transferred into the crucible 1 as much as possible, and synthesis reaction of silicon carbide powder is conducted.|[0055] The side wall of the graphite heating cylinder 3 extends along the vertical direction and upwards exceeds the height of the crucible cover 2. The upper insulation felt 41 is arranged between the inner walls of the graphite heating cylinder 3 extending beyond the crucible cover 2 in a stacked manner, and is stacked above the crucible cover 2 for insulating the crucible cover 2.|[0056] The crucible cover 2 is provided with a plurality of through holes 21 penetrating therethrough, and the through holes 21 allow nitrogen released by the upper insulation blanket 42 at a high temperature to enter the crucible 1 to react with the adsorbent, thereby removing nitrogen inside the upper insulation blanket 41 and the peripheral insulation blanket 42.|[0057] In some embodiments, a plurality of through holes 21 are provided in a circumferential array on the crucible cover 2.|[0058] In some embodiments, the diameter of the through hole 21 is 3-7 mm.|[0059] In some preferred embodiments, the crucible cover 2 is provided with 4 through holes 21 therethrough, the diameter of the through holes 21 being 5mm.|[0060] Example 1|[0061] The preparation method of the silicon carbide powder comprises the following steps: the method comprises a pretreatment step, a new thermal field blank burning step, a new thermal field nitrogen absorbing step and a synthesis step.|[0062] Pretreatment: 20kg of silicon carbide powder below a 40-mesh screen is taken, and about 18.5kg of 40-300-mesh silicon carbide mixed powder is obtained after passing through a 300-mesh screen. Putting 40-300 mesh silicon carbide powder into a high-purity quartz boat, feeding the high-purity quartz boat into a quartz tube furnace, introducing air, heating to 1000 ℃, and preserving heat for 6 hours to obtain about 16.2kg of pretreated silicon carbide powder, wherein the silicon carbide powder is white after Wen Chutan meshes of high silicon carbide powder are shown in figure 2.|[0063] And (3) a new thermal field blank firing step: performing blank burning treatment on the silicon carbide powder synthesis device shown in fig. 1, and raising the temperature to 1000 ℃, and maintaining the pressure at 3x 10 -5 mbar for 5 hours; the second stage was carried out by raising the temperature to 2200℃and the pressure to 3X 10 -3 mbar, maintaining for 40h, and finally cooling the new thermal field and synthesis unit.|[0064] A new thermal field nitrogen absorption step: about 8kg of the pretreated silicon carbide powder is taken and placed in a crucible shown in FIG. 1, and the crucible is added with the silicon carbide powder and heated to 2260+/-10 ℃ under the pressure of 500+/-2 mbar, and then the crucible is preserved for 40 hours. After cooling, the adsorbed silicon carbide powder was taken out and the color was observed.|[0065] The synthesis steps are as follows: uniformly mixing silicon powder with the median particle size D50=500 mu m and graphite powder with the median particle size D50=30 mu m according to the proportion of 1.1:1 of silicon-carbon molar ratio, and then placing the mixture into a crucible, heating the crucible to 1000 ℃ and maintaining the pressure at 5 x 10 -5 mbar for 5 hours; then continuously heating to 2050+/-10 ℃ and preserving heat for 40 hours, introducing argon into the crucible to enable the pressure to reach 200+/-2 mbar, and reacting for 30 hours to obtain massive silicon carbide;|[0066] Crushing and grinding the massive silicon carbide, screening, removing carbon, cleaning and drying to obtain 8-40# high-purity silicon carbide powder. |[0067] Example 2|[0068] Example 2 differs from example 1 in that example 2 repeats the new thermal field nitrogen absorption step once, i.e., after the first new thermal field nitrogen absorption step is completed, the second new thermal field nitrogen absorption step is performed again using the pretreated silicon carbide powder.|[0069] The specific new thermal field nitrogen absorption step is operated as follows: about 8kg of the pretreated silicon carbide powder is taken and placed in a crucible shown in FIG. 1, and the crucible is added with the silicon carbide powder and heated to 2260+/-10 ℃ under the pressure of 500+/-2 mbar, and then the crucible is preserved for 40 hours. And cooling, taking out the adsorbed silicon carbide powder, putting the pretreated silicon carbide powder into the crucible again, repeating the nitrogen absorption step of the new thermal field, carrying out the second adsorption, and finally observing the color of the silicon carbide powder after the first adsorption and the color of the silicon carbide powder after the second adsorption respectively.|[0070] The color of the silicon carbide powder after the first adsorption is shown in fig. 3, and the color of the silicon carbide powder after the second adsorption is shown in fig. 4.|[0071] The remaining preparation steps are identical to those of example 1.|[0072] Example 3|[0073] Example 3 differs from example 1 in that the silicon carbide powder manufacturing method of example 3 includes only the pretreatment step, the new thermal field nitrogen-absorbing step, and the synthesis step, and does not include the new thermal field idle firing step.|[0074] Example 4|[0075] Example 4 differs from example 2 in that example 4 sifts 80-300 mesh silicon carbide powder as an adsorbent in the pretreatment step, and the remaining preparation steps are the same as in example 2.|[0076] Comparative example 1|[0077] The synthesis of the silicon carbide powder was directly performed, i.e., only the synthesis procedure in example 1 was performed, and the resulting silicon carbide powder was synthesized.|[0078] Comparative example 2|[0079] In comparative example 2, silicon carbide powder was synthesized by introducing a high purity inert gas into a crucible and taking out nitrogen in a synthesizing apparatus with the inert gas.|[0080] Comparative example 3|[0081] Comparative example 3 is different from example 1 in that the silicon carbide powder manufacturing method of comparative example 3 does not include a pretreatment step and a new thermal field nitrogen-absorbing step, i.e., comparative example 3 is subjected to a new thermal field idle firing step and a synthesis step, and the resultant silicon carbide powder is synthesized.|[0082] Comparative example 4|[0083] Comparative example 4 is different from example 1 in that the silicon carbide powder manufacturing method of comparative example 3 does not include a pretreatment step, that is, a new thermal field blank firing step, a new thermal field nitrogen-absorbing step, and a synthesis step are performed, wherein the adsorbent used in the new thermal field nitrogen-absorbing step is 80 to 300 mesh silicon carbide powder, and is black.|[0084] Performance testing|[0085] 1. And (3) color observation: the color of the silicon carbide powder was observed, wherein the silicon carbide powder prepared in example 1 is shown in fig. 5; the silicon carbide powder prepared in example 2 is shown in FIG. 6; the silicon carbide powder obtained in comparative example 1 is shown in fig. 7.|[0086] 2. And detecting the purity of the synthesized silicon carbide powder.|[0087] 3. The duty ratio of the synthesized silicon carbide powder 8 to 40# was detected.|[0088] The results of the performance tests of each example and each comparative example are recorded in table 1 below.|[0089] Table 1 results of performance testing of each example and each comparative example|[0090] ProjectSilicon carbide powder colorSilicon carbide powder purityNitrogen content (at/cm 3)8-40# Duty cycleExample 1Green colour99.99993%2.32*e1873.2%Example 2Light green99.99994%4.65*e1772.5%Example 3Green colour99.99992%3.32*e1873.5%Example 4Light green99.99995%8.65*e1672.8%Comparative example 1Dark green99.99992%7.76*e1971.9%Comparative example 2Dark green99.99993%6.76*e1973.0%Comparative example 3Dark green99.99992%5.46*e1972.2%Comparative example 4Dark green99.99994%1.96*e1972.8%|[0091] According to the nitrogen absorption treatment method for the new thermal field of the PVT furnace synthetic silicon carbide powder, nitrogen in the new thermal field can be well absorbed and removed by analyzing the performance test results of the examples 1-4. In addition, after the pretreatment step, a new thermal field blank firing step is set, a new thermal field nitrogen absorbing step is repeated for a plurality of times, and silicon carbide powder with 80-300 meshes is selected as an adsorbent, so that the adsorption effect can be further improved, and the nitrogen content in the silicon carbide powder is reduced.|[0092] According to the nitrogen adsorption treatment method for the new thermal field for synthesizing the silicon carbide powder by the PVT furnace, provided by the application, the adsorption effect of nitrogen can be simply judged through the color change of the adsorbent before and after the nitrogen adsorption step of the new thermal field.|[0093] According to the analysis of the performance test results of the comparative example 1 and the comparative example 2, the comparative example 1 is directly synthesized into silicon carbide powder without nitrogen absorption treatment, the conventional nitrogen removal mode is adopted by introducing inert gas into the device in the comparative example 2, the effect of the two nitrogen absorption treatment methods is lower than that of the nitrogen absorption method, the obtained silicon carbide powder has higher nitrogen content, the resistivity of the silicon nitride single crystal discharged from the subsequent growth is unqualified, and the economic loss is caused.|[0094] As can be seen from the comparison of the performance test results of the example 1 and the comparative example 3, the nitrogen removal cannot be achieved only by the new thermal field blank firing step, and the silicon carbide powder is used as an adsorbent to better adsorb and remove nitrogen in the new thermal field, so that the purity of the silicon carbide powder is improved.|[0095] As can be seen from comparison of the performance test results of the example 1 and the comparative example 4, the pretreatment step of the adsorbent can remove carbon powder in silicon carbide, and a silicon-rich atmosphere is generated in the nitrogen-absorbing treatment process of the new thermal field, so that the nitrogen-absorbing capacity of the adsorbent is improved.|[0096] The nitrogen-absorbing treatment method for the new thermal field of the PVT furnace synthesized silicon carbide powder has good nitrogen-removing effect, so that the nitrogen content in the PVT furnace synthesized silicon carbide powder can meet the requirement of crystal production.|[0097] The foregoing has outlined the basic principles, features, and advantages of the present application. It will be understood by those skilled in the art that the present application is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present application, and various changes and modifications may be made therein without departing from the spirit and scope of the application, which is defined by the appended claims. The scope of the application is defined by the appended claims and equivalents thereof. (CN117585678)|TECHNICAL FIELD|Technical Field|[0001] The application relates to the technical field of silicon carbide synthesis, in particular to a nitrogen absorption treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace.|BACKGROUND ART|[0002] Silicon carbide (SiC) is a popular material for third generation semiconductors, and is widely used in industries such as 5G communication, new energy automobiles, photovoltaic inverters, and the like, due to its excellent characteristics of wide forbidden band, high saturated electron mobility, high breakdown electric field, high thermal conductivity, and the like.|[0003] The synthesis method of the high-purity silicon carbide powder used for the growth of the third-generation semiconductor silicon carbide single crystal comprises the following steps: liquid phase, solid phase and gas phase processes. The solid phase method (improving the self-propagating method to synthesize the silicon carbide is also called PVT method) is used for preparing the high-purity silicon carbide, and has the characteristics of high purity, high yield, good particle crystallinity and the like, and is widely popularized.|[0004] The growth raw materials of the silicon carbide crystal are that after the high-purity silicon powder and carbon powder are uniformly mixed, the mixture is filled into a graphite crucible, then the crucible is filled into a new thermal field, the new thermal field is put into a PVT furnace and heated to 2000-2200 ℃ to react and synthesize high-purity silicon carbide blocks, and finally the silicon carbide powder with the required mesh number is prepared through the procedures of crushing, grinding, screening, decarbonizing, cleaning, drying and the like.|[0005] When the PVT method is adopted to grow the silicon carbide powder, the novel heat-insulating material adsorbs a large amount of nitrogen in the preparation process, and when the silicon carbide powder is synthesized at a high temperature, the materials release the nitrogen adsorbed in the interior, so that the nitrogen content in the grown silicon carbide powder is higher. The silicon carbide powder adsorbs excessive nitrogen, and the color of the silicon carbide powder is black or dark greenish black, so that the silicon carbide powder cannot be used for synthesizing silicon carbide single crystal growth.|[0006] Silicon carbide powder for silicon carbide single crystal growth requires low metal and nitrogen content, and has extremely high nitrogen content, and the excessive nitrogen content can cause unqualified resistivity of the silicon carbide single crystal to be grown and discharged, so that economic loss is caused. Therefore, there is a need for a nitrogen removal process for silicon carbide crystal growth materials that is economical, simple and easy to operate, reduces the nitrogen content in the silicon carbide growth materials, and improves the stability of the resistivity of subsequent silicon carbide crystals.|DISCLOSURE|Disclosure of Invention|[0007] The application aims to reduce the nitrogen content in the new thermal field graphite soft felt, so that the nitrogen content in the silicon carbide powder synthesized by a PVT furnace can meet the requirement of crystal production.|[0008] In order to achieve the above purpose, the application adopts the following technical scheme: a nitrogen-absorbing treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace comprises the following steps of: carrying out high Wen Chutan on the adsorbent to obtain a pretreated adsorbent; a new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating, pressurizing and maintaining for a period of time, cooling and taking out the adsorbent; the synthesis steps are as follows: uniformly mixing silicon powder and graphite powder, placing the mixture in a crucible of a new thermal field to perform a synthesis reaction of silicon carbide powder to obtain massive silicon carbide, crushing, grinding, screening, decarbonizing, cleaning and drying the silicon carbide to obtain the silicon carbide powder which can be used for silicon carbide single crystal growth; the adsorbent is silicon carbide.|[0009] Preferably, the adsorbent is 40 to 300 mesh silicon carbide powder.|[0010] As another preferable aspect, the adsorbent is 80 to 300 mesh silicon carbide powder.|[0011] As another preference, the adsorbent is the product of the synthesis step.|[0012] As another preference, the nitrogen content of the adsorbent is less than 5*e 16 at/cm3.|[0013] As another preferable aspect, the adsorbent has a purity of 99.9999% or more.|[0014] As another preferable mode, the temperature of the new thermal field nitrogen absorbing step is set to 2000-2200 ℃, the pressure is 100-500 mbar, and the heat preservation time is 20-40 h.|[0015] As another preferable, the pretreatment step specifically includes: and placing the adsorbent in a quartz tube furnace, introducing air into the furnace, heating to 900-1000 ℃, and keeping the temperature for 6-8 hours.|[0016] As another preferable mode, the synthesizing step specifically includes: the silicon powder and the graphite powder are mixed according to the silicon-carbon molar ratio of (1-1.1): 1 are evenly mixed and placed in a crucible of a new thermal field, the temperature is 2000-2200 ℃, the pressure is 0-800 mbar, the reaction time is 20-50 h, and the synthesis reaction of silicon carbide is carried out, thus obtaining the massive silicon carbide.|[0017] As another preferable mode, the method further comprises a new thermal field blank firing step after the pretreatment step, wherein the new thermal field blank firing step specifically comprises the following steps: placing the crucible in a new thermal field, heating and pressurizing the new thermal field and the crucible for a period of time, and finally cooling the crucible and the new thermal field.|[0018] Compared with the prior art, the application has the beneficial effects that:|[0019] (1) According to the application, 40-300 meshes of silicon carbide powder is used as an adsorbent, and Si and SiC 2 components are evaporated through the silicon carbide powder, so that nitrogen in the device can be well adsorbed, and the nitrogen content in the silicon carbide powder is reduced; |[0020] (2) The application adopts the silicon carbide powder as the adsorbent, can simply judge the adsorption effect by observing the color of the adsorbent, and the silicon carbide powder with 40-300 meshes is waste material after the synthesis step, so that the adsorbent is not required to be purchased additionally, and the economic cost is saved. |DRAWINGS DESCRIPTION|[0021] FIG. 1 is a schematic view of an apparatus for manufacturing silicon carbide powder according to an embodiment of the present application;|[0022] FIG. 2 is a digital photograph of the adsorbent silicon carbide after the pretreatment step of example 1 of the present application; |[0023] FIG. 3 is a digital photograph of the adsorbent silicon carbide after the first new thermal field nitrogen gettering step of example 2 of the present application; |[0024] FIG. 4 is a digital photograph of the adsorbent silicon carbide after the second new thermal field nitrogen gettering step of example 2 of the present application; |[0025] FIG. 5 is a digital photograph of silicon carbide powder prepared in example 1 of the present application; |[0026] FIG. 6 is a digital photograph of silicon carbide powder prepared in example 2 of the present application; |[0027] FIG. 7 is a digital photograph of silicon carbide powder prepared in comparative example 1 of the present application; |[0028] in the figure: 1. a crucible; 2. a crucible cover; 21. a through hole; 3. a graphite heating cylinder; 4. graphite insulation felt; 41. a thermal insulation felt is arranged on the upper surface; 42. and a peripheral heat insulation felt. |INVENTION MODE|Detailed Description|[0029] The present application will be further described with reference to the following specific embodiments, and it should be noted that, on the premise of no conflict, new embodiments may be formed by any combination of the embodiments or technical features described below.|[0030] The terms "comprises" and "comprising," along with any variations thereof, in the description and claims, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.|[0031] The application provides a nitrogen-absorbing treatment method for a new thermal field for synthesizing silicon carbide powder by a PVT furnace, which comprises a pretreatment step, a new thermal field nitrogen-absorbing step and a synthesis step.|[0032] Pretreatment: carrying out high Wen Chutan on the adsorbent to obtain a pretreated adsorbent;|[0033] A new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating, pressurizing and maintaining for a period of time, cooling and taking out the adsorbent; |[0034] The synthesis steps are as follows: and (3) uniformly mixing the silicon powder and the graphite powder, placing the mixture into a crucible of a new thermal field to perform a synthesis reaction of silicon carbide powder to obtain massive silicon carbide, and then crushing, grinding, screening, decarbonizing, cleaning and drying the massive silicon carbide to obtain the silicon carbide powder which can be used as a growth raw material for growing silicon carbide single crystals. |[0035] In some embodiments, the adsorbent is 40-300 mesh silicon carbide powder. The adsorbent is silicon carbide powder, si and SiC 2 components are evaporated from the silicon carbide powder at high temperature, and simultaneously nitrogen is slowly released from growth equipment, graphite pieces and heat insulation materials in a high-temperature environment, and the released nitrogen is captured by Si and SiC 2 steam, so that the nitrogen is adsorbed in a new thermal field nitrogen adsorption step.|[0036] The silicon carbide powder with 40-300 meshes is used as the adsorbent, the specific surface area of the powder is large, the nitrogen content is low, and the rest silicon carbide powder except for sublimation of the silicon carbide powder can also play a role in adsorption.|[0037] In addition, the adsorbent is silicon carbide powder with 40-300 meshes, so that waste materials in the production link can be utilized, the adsorbent is not required to be purchased additionally, and the economic cost can be saved. After the synthesis of the synthesis step is finished, crushing massive silicon carbide, grinding the massive silicon carbide into particles, and sieving the particles to obtain 8-40-mesh silicon carbide powder serving as a growth raw material for growing silicon carbide single crystals, wherein the rest 40-mesh silicon carbide powder can be used as an adsorbent in the pretreatment step after sieving, so that the raw material is saved, and the method is economical and environment-friendly.|[0038] In some preferred embodiments, after the new thermal field nitrogen absorption step is completed, the color of the adsorbent is observed, and if the adsorbent is dark green, the pretreatment step and the new thermal field nitrogen absorption step may be repeated multiple times until the adsorbent color is light green, indicating that most of the nitrogen in the new thermal field is removed, and the synthesis step may be performed.|[0039] The adsorbent uses silicon carbide powder, the color of the 40-300 mesh silicon carbide powder obtained by screening is black, and the color of the silicon carbide powder becomes white after the pretreatment step is carried out, and the height of the silicon carbide powder is Wen Chutan. After the silicon carbide powder adsorbs nitrogen, the color is changed from white to dark green or even black, so that the silicon carbide powder is used as the adsorbent, and whether the nitrogen in the device is reduced to a state capable of synthesizing the universal crystal raw material can be judged through the color change of the adsorbent after the new thermal field nitrogen adsorption step. That is, the color of the adsorbent is observed after the new thermal field nitrogen adsorption step, if the adsorbent still presents dark green, the nitrogen in the device is not completely adsorbed and removed, and the pretreatment step and the new thermal field nitrogen adsorption step can be repeated until the adsorbed adsorbent presents light green, and the nitrogen in the device is completely removed.|[0040] The application uses silicon carbide powder as the adsorbent, has better nitrogen adsorption effect, and can simply judge the nitrogen removal effect in the silicon carbide powder synthesis device through the color change of the adsorbent, thereby ensuring that the synthesized silicon carbide powder with high purity is used as the growth raw material of silicon carbide single crystals.|[0041] In some embodiments, the adsorbent is 40-300 mesh (national standard) silicon carbide powder having a purity of 99.9999% or greater.|[0042] In some embodiments, the adsorbent is 40-300 mesh (national standard) silicon carbide powder having a nitrogen content of less than 5*e 16at/cm3.|[0043] In some preferred embodiments, the adsorbent is 80-300 mesh silicon carbide powder, with better adsorption.|[0044] In some embodiments, the temperature of the new thermal field nitrogen absorption step is set to 2000-2200 ℃, the pressure is set to 100-500 mbar, and the heat preservation time is 20-40 h.|[0045] In some embodiments, the method of manufacturing silicon carbide powder further comprises a new thermal field blank firing step disposed after the pretreatment step and before the new thermal field nitrogen gettering step.|[0046] And (3) a new thermal field blank firing step: placing the crucible in a new thermal field, heating and pressurizing the crucible in the new thermal field for a period of time, and finally cooling the crucible and the new thermal field.|[0047] In some embodiments, the new thermal field blank firing step uses the new thermal field to heat and pressurize the crucible in two stages of heat and pressure. Heating to 1000-1200 deg.c in the first stage with pressure below 5x 10 -5 mbar and maintaining for 2-5 hr; in the second stage, the temperature is raised to 2000-2200 ℃, the pressure is maintained below 5x 10 -3 mbar, the maintaining time is 20-40 h, and finally the new thermal field and the crucible are cooled.|[0048] The empty burning step mainly aims at utilizing negative pressure and high temperature to discharge nitrogen adsorbed in the new thermal field material through heating and pressurizing, so that the nitrogen in the new thermal field is primarily removed, and the using amount of the adsorbent in the later stage is saved.|[0049] In some embodiments, the pretreatment step comprises placing the adsorbent in a quartz tube furnace, introducing air into the tube furnace, heating to 900-1000 ℃, and maintaining the temperature for 6-8 hours to obtain the pretreated adsorbent, wherein the color of the pretreated adsorbent is white.|[0050] In some embodiments, the synthesis step comprises mixing silicon powder and graphite powder in a molar ratio of Si to C of (1 to 1.1): 1, uniformly mixing, placing the mixture into a crucible of a new thermal field to perform a synthesis reaction of silicon carbide powder, wherein the temperature is 2000-2200 ℃, and filling inert gas into a reaction device to control the pressure to be 0-800 mbar, wherein the synthesis reaction time is 20-50 h, so as to obtain silicon carbide agglomerates.|[0051] In some preferred embodiments, the median particle diameter D50 of the silicon powder is 0.3-3 mm, and the purity is greater than or equal to 99.9999%; the median particle diameter D50 of the graphite powder is 20-200 mu m, and the purity is more than or equal to 99.9999%.|[0052] In some embodiments, the inert gas in the synthesis step is high purity argon having a nitrogen content of less than 5 x 10 -3 ppm and a purity of 99.9999% or greater.|[0053] As shown in FIG. 1, the application also provides a silicon carbide powder synthesizing device for silicon carbide single crystal growth, which comprises a crucible 1 and a crucible cover 2 above the crucible 1, wherein a graphite heating cylinder 3 for heating is arranged outside the crucible 1, and a graphite heat preservation felt 4 for heat preservation is arranged outside the graphite heating cylinder 3.|[0054] The graphite heating cylinder 3 is tightly attached to the outer wall and the bottom of the crucible 1, so that the graphite heating cylinder 3 can rapidly transfer heat to the crucible 1, and heat loss is reduced. The graphite heat preservation felt 4 comprises an upper heat preservation felt 41 and a peripheral heat preservation felt 42, wherein the peripheral heat preservation felt 42 is arranged on the outer side of the graphite heating cylinder 3 in a surrounding mode, heat preservation is conducted on the outer side of the graphite heating cylinder 3, temperature loss is avoided, heat is transferred into the crucible 1 as much as possible, and synthesis reaction of silicon carbide powder is conducted.|[0055] The side wall of the graphite heating cylinder 3 extends along the vertical direction and upwards exceeds the height of the crucible cover 2. The upper insulation felt 41 is arranged between the inner walls of the graphite heating cylinder 3 extending beyond the crucible cover 2 in a stacked manner, and is stacked above the crucible cover 2 for insulating the crucible cover 2.|[0056] The crucible cover 2 is provided with a plurality of through holes 21 penetrating therethrough, and the through holes 21 allow nitrogen released by the upper insulation blanket 42 at a high temperature to enter the crucible 1 to react with the adsorbent, thereby removing nitrogen inside the upper insulation blanket 41 and the peripheral insulation blanket 42.|[0057] In some embodiments, a plurality of through holes 21 are provided in a circumferential array on the crucible cover 2.|[0058] In some embodiments, the diameter of the through hole 21 is 3-7 mm.|[0059] In some preferred embodiments, the crucible cover 2 is provided with 4 through holes 21 therethrough, the diameter of the through holes 21 being 5mm.|[0060] Example 1|[0061] The preparation method of the silicon carbide powder comprises the following steps: the method comprises a pretreatment step, a new thermal field blank burning step, a new thermal field nitrogen absorbing step and a synthesis step.|[0062] Pretreatment: 20kg of silicon carbide powder below a 40-mesh screen is taken, and about 18.5kg of 40-300-mesh silicon carbide mixed powder is obtained after passing through a 300-mesh screen. Putting 40-300 mesh silicon carbide powder into a high-purity quartz boat, feeding the high-purity quartz boat into a quartz tube furnace, introducing air, heating to 1000 ℃, and preserving heat for 6 hours to obtain about 16.2kg of pretreated silicon carbide powder, wherein the silicon carbide powder is white after Wen Chutan meshes of high silicon carbide powder are shown in figure 2.|[0063] And (3) a new thermal field blank firing step: performing blank burning treatment on the silicon carbide powder synthesis device shown in fig. 1, and raising the temperature to 1000 ℃, and maintaining the pressure at 3x 10 -5 mbar for 5 hours; the second stage was carried out by raising the temperature to 2200℃and the pressure to 3X 10 -3 mbar, maintaining for 40h, and finally cooling the new thermal field and synthesis unit.|[0064] A new thermal field nitrogen absorption step: about 8kg of the pretreated silicon carbide powder is taken and placed in a crucible shown in FIG. 1, and the crucible is added with the silicon carbide powder and heated to 2260+/-10 ℃ under the pressure of 500+/-2 mbar, and then the crucible is preserved for 40 hours. After cooling, the adsorbed silicon carbide powder was taken out and the color was observed.|[0065] The synthesis steps are as follows: uniformly mixing silicon powder with the median particle size D50=500 mu m and graphite powder with the median particle size D50=30 mu m according to the proportion of 1.1:1 of silicon-carbon molar ratio, and then placing the mixture into a crucible, heating the crucible to 1000 ℃ and maintaining the pressure at 5 x 10 -5 mbar for 5 hours; then continuously heating to 2050+/-10 ℃ and preserving heat for 40 hours, introducing argon into the crucible to enable the pressure to reach 200+/-2 mbar, and reacting for 30 hours to obtain massive silicon carbide;|[0066] Crushing and grinding the massive silicon carbide, screening, removing carbon, cleaning and drying to obtain 8-40# high-purity silicon carbide powder. |[0067] Example 2|[0068] Example 2 differs from example 1 in that example 2 repeats the new thermal field nitrogen absorption step once, i.e., after the first new thermal field nitrogen absorption step is completed, the second new thermal field nitrogen absorption step is performed again using the pretreated silicon carbide powder.|[0069] The specific new thermal field nitrogen absorption step is operated as follows: about 8kg of the pretreated silicon carbide powder is taken and placed in a crucible shown in FIG. 1, and the crucible is added with the silicon carbide powder and heated to 2260+/-10 ℃ under the pressure of 500+/-2 mbar, and then the crucible is preserved for 40 hours. And cooling, taking out the adsorbed silicon carbide powder, putting the pretreated silicon carbide powder into the crucible again, repeating the nitrogen absorption step of the new thermal field, carrying out the second adsorption, and finally observing the color of the silicon carbide powder after the first adsorption and the color of the silicon carbide powder after the second adsorption respectively.|[0070] The color of the silicon carbide powder after the first adsorption is shown in fig. 3, and the color of the silicon carbide powder after the second adsorption is shown in fig. 4.|[0071] The remaining preparation steps are identical to those of example 1.|[0072] Example 3|[0073] Example 3 differs from example 1 in that the silicon carbide powder manufacturing method of example 3 includes only the pretreatment step, the new thermal field nitrogen-absorbing step, and the synthesis step, and does not include the new thermal field idle firing step.|[0074] Example 4|[0075] Example 4 differs from example 2 in that example 4 sifts 80-300 mesh silicon carbide powder as an adsorbent in the pretreatment step, and the remaining preparation steps are the same as in example 2.|[0076] Comparative example 1|[0077] The synthesis of the silicon carbide powder was directly performed, i.e., only the synthesis procedure in example 1 was performed, and the resulting silicon carbide powder was synthesized.|[0078] Comparative example 2|[0079] In comparative example 2, silicon carbide powder was synthesized by introducing a high purity inert gas into a crucible and taking out nitrogen in a synthesizing apparatus with the inert gas.|[0080] Comparative example 3|[0081] Comparative example 3 is different from example 1 in that the silicon carbide powder manufacturing method of comparative example 3 does not include a pretreatment step and a new thermal field nitrogen-absorbing step, i.e., comparative example 3 is subjected to a new thermal field idle firing step and a synthesis step, and the resultant silicon carbide powder is synthesized.|[0082] Comparative example 4|[0083] Comparative example 4 is different from example 1 in that the silicon carbide powder manufacturing method of comparative example 3 does not include a pretreatment step, that is, a new thermal field blank firing step, a new thermal field nitrogen-absorbing step, and a synthesis step are performed, wherein the adsorbent used in the new thermal field nitrogen-absorbing step is 80 to 300 mesh silicon carbide powder, and is black.|[0084] Performance testing|[0085] 1. And (3) color observation: the color of the silicon carbide powder was observed, wherein the silicon carbide powder prepared in example 1 is shown in fig. 5; the silicon carbide powder prepared in example 2 is shown in FIG. 6; the silicon carbide powder obtained in comparative example 1 is shown in fig. 7.|[0086] 2. And detecting the purity of the synthesized silicon carbide powder.|[0087] 3. The duty ratio of the synthesized silicon carbide powder 8 to 40# was detected.|[0088] The results of the performance tests of each example and each comparative example are recorded in table 1 below.|[0089] Table 1 results of performance testing of each example and each comparative example|[0090] ProjectSilicon carbide powder colorSilicon carbide powder purityNitrogen content (at/cm 3)8-40# Duty cycleExample 1Green colour99.99993%2.32*e1873.2%Example 2Light green99.99994%4.65*e1772.5%Example 3Green colour99.99992%3.32*e1873.5%Example 4Light green99.99995%8.65*e1672.8%Comparative example 1Dark green99.99992%7.76*e1971.9%Comparative example 2Dark green99.99993%6.76*e1973.0%Comparative example 3Dark green99.99992%5.46*e1972.2%Comparative example 4Dark green99.99994%1.96*e1972.8%|[0091] According to the nitrogen absorption treatment method for the new thermal field of the PVT furnace synthetic silicon carbide powder, nitrogen in the new thermal field can be well absorbed and removed by analyzing the performance test results of the examples 1-4. In addition, after the pretreatment step, a new thermal field blank firing step is set, a new thermal field nitrogen absorbing step is repeated for a plurality of times, and silicon carbide powder with 80-300 meshes is selected as an adsorbent, so that the adsorption effect can be further improved, and the nitrogen content in the silicon carbide powder is reduced.|[0092] According to the nitrogen adsorption treatment method for the new thermal field for synthesizing the silicon carbide powder by the PVT furnace, provided by the application, the adsorption effect of nitrogen can be simply judged through the color change of the adsorbent before and after the nitrogen adsorption step of the new thermal field.|[0093] According to the analysis of the performance test results of the comparative example 1 and the comparative example 2, the comparative example 1 is directly synthesized into silicon carbide powder without nitrogen absorption treatment, the conventional nitrogen removal mode is adopted by introducing inert gas into the device in the comparative example 2, the effect of the two nitrogen absorption treatment methods is lower than that of the nitrogen absorption method, the obtained silicon carbide powder has higher nitrogen content, the resistivity of the silicon nitride single crystal discharged from the subsequent growth is unqualified, and the economic loss is caused.|[0094] As can be seen from the comparison of the performance test results of the example 1 and the comparative example 3, the nitrogen removal cannot be achieved only by the new thermal field blank firing step, and the silicon carbide powder is used as an adsorbent to better adsorb and remove nitrogen in the new thermal field, so that the purity of the silicon carbide powder is improved.|[0095] As can be seen from comparison of the performance test results of the example 1 and the comparative example 4, the pretreatment step of the adsorbent can remove carbon powder in silicon carbide, and a silicon-rich atmosphere is generated in the nitrogen-absorbing treatment process of the new thermal field, so that the nitrogen-absorbing capacity of the adsorbent is improved.|[0096] The nitrogen-absorbing treatment method for the new thermal field of the PVT furnace synthesized silicon carbide powder has good nitrogen-removing effect, so that the nitrogen content in the PVT furnace synthesized silicon carbide powder can meet the requirement of crystal production.|[0097] The foregoing has outlined the basic principles, features, and advantages of the present application. It will be understood by those skilled in the art that the present application is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present application, and various changes and modifications may be made therein without departing from the spirit and scope of the application, which is defined by the appended claims. The scope of the application is defined by the appended claims and equivalents thereof. Family Number|(108619719)|108619719|Abstract|(CN117585678B B)|The invention discloses a nitrogen absorption treatment method for a new thermal field for synthesizing silicon carbide powder in a PVT furnace , and the treatment method comprises the following steps : a pretreatment step : carrying out high - temperature carbon removal on an adsorbent to obtain a pretreated adsorbent ; a new thermal field nitrogen absorption step : placing the pretreated adsorbent in a crucible of a new thermal field , heating and pressurizing , maintaining for a period of time , cooling , and taking out the adsorbent ; the synthesis method comprises the following steps : uniformly mixing silicon powder and graphite powder , putting the mixture into a crucible of a new thermal field , carrying out a synthesis reaction of silicon carbide powder to obtain blocky silicon carbide , and crushing , grinding , screening , decarbonizing , cleaning and drying the silicon carbide to obtain the silicon carbide powder which can be used for silicon carbide single crystal growth . The adsorbent selected by the invention is silicon carbide , so that the economic cost is saved , and the nitrogen removal effect is good . |CPC codes|(CN117585678B B)|B01D - 053/02 |B01D - 2257/102 |B01J - 020/02/59 |C01B - 032/984 |IPC codes|(CN117585678B B)|B01D - 053/02 |B01J - 020/02 |C01B - 032/984 | Chemical engineering|Environmental technology|Materials, metallurgy|Thermal processes and apparatus B01D-053/02|B01D-2257/102|B01J-020/02/59|C01B-032/984|F27D-017/20 B01D-053/02|B01D-2257/102|B01J-020/02/59|C01B-032/984|F27D-017/20 B01D-053/02|B01J-020/02|C01B-032/984|F27D-017/00 B01D-053/02|B01J-020/02|C01B-032/984|F27D-017/00 WO202077846|CN116789137|WO2023201934|CN109280966|JP2019151533|CN108118394|KR20160089973|JP2009173501|JP2008120619|US20050022727|CN1351680|US5718760|US5611955|US5119540|CN115872405|CN113005510|CN109280965|KR20140141978 WO202077846 88400614 WHO=Examiner SELF=N CAT=X|CN116789137 106609971 WHO=Examiner SELF=N CAT=A|WO2023201934 100158278 WHO=Examiner SELF=N CAT=A|CN109280966 83230099 WHO=Examiner SELF=N CAT=A|JP2019151533 85987177 WHO=Examiner SELF=N CAT=A|CN108118394 79921141 WHO=Examiner SELF=N CAT=A|KR20160089973 73781532 WHO=Examiner SELF=N CAT=A|JP2009173501 32950802 WHO=Examiner SELF=N CAT=A|JP2008120619 32754409 WHO=Examiner SELF=N CAT=A|US20050022727 1029937 WHO=Examiner SELF=N CAT=A|CN1351680 801555 WHO=Examiner SELF=N CAT=A|US5718760 43170779 WHO=Examiner SELF=N CAT=A|US5611955 14753713 WHO=Examiner SELF=N CAT=A|US5119540 42728429 WHO=Examiner SELF=N CAT=A|CN115872405 104389909 WHO=Examiner SELF=Y|CN113005510 94860145 WHO=Examiner SELF=N|CN109280965 83213186 WHO=Examiner SELF=N|KR20140141978 68636125 WHO=Examiner SELF=N US5119540; US5611955; US5718760; CN1351680; US20050022727; JP2008120619; JP2009173501; KR20160089973; CN108118394; CN109280966; JP2019151533; CN116789137; WO2023201934; WO202077846; CN109280965; CN113005510; CN115872405; KR20140141978; WO2020077846 GRANTED (CN117585678)|GRANTED ALIVE (CN117585678)|ALIVE (CN117585678)|LEGAL DETAILS FOR CN117585678|Actual or expected expiration date=2043-11-30|Legal state=ALIVE|Status=GRANTED|Event publication date=2023-11-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202311616678|Application date=2023-11-30|Standardized application number=2023CN-1616678|Event publication date=2024-02-23|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN117585678|Publication stage code=A|Publication date=2024-02-23|Standardized publication number=CN117585678|Event publication date=2024-02-23|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-03-12|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-08-27|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN117585678|Publication stage code=B|Publication date=2024-08-27|Standardized publication number=CN117585678B|Event publication date=2024-08-27|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2025-08-12|Event code=CN/CP03|Event group=Change of name or address Reassignment|Change in the name or address of the patentee|FORMER APPLICANT:NINGBO HESHENG NEW MAT CO LTD APPLICANT:Ningbo Alpha Semiconductor Co., Ltd. (CN117585678)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRjzmtaUwR98xj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000074172371&ekey=2250&xpn=CN117585678B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=i1nXqb0RZ%252BUPfzoHG%252FMXebmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN117585678)|CN|(CN117585678)|CN (CN117585678)|NAME=NINGBO HESHENG NEW MAT CO LTD , COUNTRY=CN|(CN117585678)|NAME=NINGBO HESHENG NEW MAT CO LTD , COUNTRY=CN (CN117585678)|NAME=YUAN HONGBO;NINGBO YONGXIN HECHUANG INTELLECTUAL PROPERTY AGENCY CO., LTD , REG=33552|(CN117585678)|NAME=YUAN HONGBO;NINGBO YONGXIN HECHUANG INTELLECTUAL PROPERTY AGENCY CO., LTD , REG=33552 (CN117585678)|CN| (CN117585678)|NAME=Zhang Wenzhong No. 1999-9, Zhouxi Road, Zhouxiang Town, Cixi City, Ningbo City, Zhejiang Province 315300 cixi city, CITY=Ningbo City, POSTCODE=315300, STATE=Zhejiang Province , COUNTRY=CN |NAME=Hao Han|NAME=Zhao Xintian|(CN117585678)|NAME=ZHANG WENZHONG|NAME=HAO HAN|NAME=ZHAO XINTIAN 0 1 Titre: (CN117585678)|Nitrogen absorption treatment method for new thermal field for synthesizing silicon carbide powder by PVT furnace Résumé: (CN117585678)|The invention discloses a nitrogen absorption treatment method for a new thermal field for synthesizing silicon carbide powder in a PVT furnace, and the treatment method comprises the following steps: a pretreatment step: carrying out high-temperature carbon removal on an adsorbent to obtain a pretreated adsorbent; a new thermal field nitrogen absorption step: placing the pretreated adsorbent in a crucible of a new thermal field, heating and pressurizing, maintaining for a period of time, cooling, and taking out the adsorbent; the synthesis method comprises the following steps: uniformly mixing silicon powder and graphite powder, putting the mixture into a crucible of a new thermal field, carrying out a synthesis reaction of silicon carbide powder to obtain blocky silicon carbide, and crushing, grinding, screening, decarbonizing, cleaning and drying the silicon carbide to obtain the silicon carbide powder which can be used for silicon carbide single crystal growth. The adsorbent selected by the invention is silicon carbide, so that the economic cost is saved, and the nitrogen removal effect is good. 64 Abstract gpt-4o-mini no The article focuses on a method for synthesizing silicon carbide powder and nitrogen absorption treatment, which does not relate to accelerated weathering or CO₂ capture.
64 CN201610704069 CN201610704069 CN106276907 75072744 CN106276907 A 2017-01-04 [CN106276907] 2016-08-23 2016-08-23 2017-01-04 (CN106276907)|2018-08-28 (CN106276907)|Treatment method of silicon carbide fine powder for lightning arrester (CN106276907)|The invention provides a treatment method of silicon carbide fine powder for a lightning arrester. The treatment method includes the treatment steps that 1, a silicon carbide raw material is preliminarily crushed through a jaw crusher, and then the material is put in an impact crusher to be secondarily crushed; 2, after silicon carbide is washed with clear water, silicon carbide is dried and put in a screener for impurity screening-out, and silicon carbide is put in a magnetic separator to be screened; 3, water is added, the material is blended into mixed paste, after concentrated sulfuric acid is added and stirring is carried out, sodium hydroxide is added, stirring is carried out while adding is carried out, finally, a carbon removal agent is added, after the material is mixed and stirred, silicon carbide is filtered out through classification sedimentation, and silicon carbide is washed with clear water; 4, silicon carbide treated in the step 3 is put in a heating furnace for high-temperature baking, after silicon carbide is baked, ventilation is carried out for natural cooling, and then airflow flotation classification is carried out. The treatment method has the advantages that multiple impurity removal and refining processes are adopted, the treated silicon carbide powder is high in purity and fine in granularity, and when a lightning arrester valve block is produced in the following process, the process temperature can be effectively reduced, and the quality of the valve block is improved. HUAIYUAN COUNTY JINHAO ELECTRONIC TECHNOLOGY (CN106276907)|HUAIYUAN COUNTY JINHAO ELECTRONIC TECHNOLOGY CO.,LTD. YAO KUN|YAO WANG|WANG CHUANWEN (CN106276907)|YAO KUN|YAO WANG|WANG CHUANWEN (CN106276907)|The invention has the advantages and positive effects that:| (CN106276907)|1. A method for processing silicon carbide fine powder for a lightning arrester is characterized by comprising the following processing steps:(1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the granularity of the crushed raw material is required to reach 5-10 mm;(2) washing the crushed silicon carbide with clear water for 3-5 times, drying, sieving in a sieving machine to remove impurities, and then screening for 2-4 times in a magnetic separator;(3) adding water into the screened silicon carbide to blend into mixed slurry with the concentration of 25-35%, adding concentrated sulfuric acid with the concentration of 98% accounting for 20-25% of the mass of the mixed slurry, stirring for 20-30 minutes, then adding sodium hydroxide, stirring while adding until the pH value of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 10-15 minutes, filtering out the silicon carbide through fractional sedimentation, and washing for 3-5 times by using clear water;(4) and (4) placing the silicon carbide treated in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature at 750-800 ℃, naturally cooling the silicon carbide by ventilation after baking for 50-60 minutes, and then carrying out airflow flotation classification on the cooled silicon carbide.| (CN106276907)|The invention aims to provide a method for treating silicon carbide fine powder for a lightning arrester. In order to realize the purpose, the invention discloses a method for processing silicon carbide fine powder for a lightning arrester, which comprises the following processing steps:|The invention discloses a method for processing silicon carbide fine powder for a lightning arrester, which comprises the following processing steps: (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the silicon carbide raw material into a counterattack crusher for secondary crushing; (2) washing silicon carbide with clear water, drying, sieving in a sieving machine to remove impurities, and sieving in a magnetic separator; (3) adding water to blend into mixed slurry, adding concentrated sulfuric acid, stirring, adding sodium hydroxide, stirring while adding, adding a carbon removing agent, mixing and stirring, performing fractional sedimentation, filtering out silicon carbide, and washing with clear water; (4) placing the silicon carbide treated in the step (3) into a heating furnace for high-temperature baking, ventilating and naturally cooling after baking, and then carrying out airflow flotation classification; the invention has the beneficial effects that: the multiple impurity removal and refinement processes are adopted, the processed silicon carbide powder is high in purity and fine in granularity, the process temperature can be effectively reduced during the subsequent production of the lightning protection device valve plate, and the quality of the valve plate is improved. Technical Field The invention relates to the technical field of silicon carbide material treatment, in particular to a method for treating silicon carbide fine powder for a lightning arrester.| (CN106276907)|SILICON CARBIDE(100,52)|FINE POWDER(100,7)|SILICON CARBIDE FINE POWDER(100,7)|FRACTIONAL SEDIMENTATION(100,6)|LIGHTNING ARRESTER(100,5)|COUNTER ATTACK CRUSHER(96,1)|FLOTATION CLASSIFICATION(94,6)|CONCENTRATED DEBACTEROL(84,6)|SILICON CARBIDE FRACTIONAL SEDIMENTATION(60,5)|MAGNETIC SEPARATOR(58,6)|SIEVING MACHINE(58,6)|MIXED SLURRY(53,11)|HEATING FURNACE(51,6)|SIEVING(48,8)|CRUSHING(47,6)|REMOVING IMPURITY(46,2)|GRANULARITY(44,1)|JAW CRUSHER(41,6)|IMPURITY(38,6)|CRUSHED RAW MATERIAL GRANULARITY(36,1)|CRUSHED SILICON CARBIDE(35,5)|SCREENED SILICON CARBIDE(34,5)|BAKING(32,6)|SILICON CARBIDE POWDER(31,3)|ACCOUNTING(31,2)|VENTILATION(31,2)|COOLED SILICON CARBIDE(26,5)|SODIUM HYDROXIDE(25,6)|BAKING TEMPERATURE(25,5)|REFINING(24,2)|SLURRY(22,4)|LIGHTNING PROTECTION(21,5)|SCREENING(21,4)|PURITY(21,3)|CLEAR WATER(18,12)|SILICON CARBIDE RAW MATERIAL(18,7)|BACK IMPACT CRUSHER(18,5)|KEROSENE(18,2)|CRUSHED RAW MATERIAL(12,5)|RAW MATERIAL(11,13)|DEVICE VALVE PLATE(10,1)|FILTERING OUT SILICON CARBIDE(10,1)|VALVE PLATE(9,6)|PROCESS TEMPERATURE(9,3)|CARRYING OUT AIRFLOW(8,6)|CARRYING OUT PRIMARY CRUSHING(7,6)|FILTERING OUT(7,1)|FINE GRANULARITY(7,1)| (CN106276907)|1. A method for processing silicon carbide fine powder for a lightning arrester is characterized by comprising the following processing steps:|(1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the granularity of the crushed raw material is required to reach 5-10 mm;|(2) washing the crushed silicon carbide with clear water for 3-5 times, drying, sieving in a sieving machine to remove impurities, and then screening for 2-4 times in a magnetic separator;|(3) adding water into the screened silicon carbide to blend into mixed slurry with the concentration of 25-35%, adding concentrated sulfuric acid with the concentration of 98% accounting for 20-25% of the mass of the mixed slurry, stirring for 20-30 minutes, then adding sodium hydroxide, stirring while adding until the pH value of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 10-15 minutes, filtering out the silicon carbide through fractional sedimentation, and washing for 3-5 times by using clear water;|(4) and (4) placing the silicon carbide treated in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature at 750-800 ℃, naturally cooling the silicon carbide by ventilation after baking for 50-60 minutes, and then carrying out airflow flotation classification on the cooled silicon carbide.|2. The method for processing the silicon carbide fine powder for the lightning arrester as claimed in claim 1, wherein the method comprises the following steps: the carbon removing agent is kerosene. (CN106276907)|TECHNICAL FIELD|[0002] The invention relates to the technical field of silicon carbide material treatment, in particular to a method for treating silicon carbide fine powder for a lightning arrester.|BACKGROUND ART|[0004] The silicon carbide is prepared by smelting quartz sand, petroleum coke, wood chips and other raw materials in a resistance furnace at high temperature, and rare minerals exist in the silicon carbide in nature. Silicon carbide can be used in many fields and is a material with high demand. The valve plate is widely applied to the field of electric appliances and can play a critical role as a valve plate in a lightning protection device.|[0005] When the valve plate is made of silicon carbide, high-temperature conditions are needed, and the temperature requirements have high requirements on equipment and processes; the fineness and purity of the silicon carbide powder is an important factor in order to reduce the process temperature at the time of its preparation.|DISCLOSURE|[0006] Disclosure of Invention|[0007] The invention aims to provide a method for treating silicon carbide fine powder for a lightning arrester.|[0008] In order to realize the purpose, the invention discloses a method for processing silicon carbide fine powder for a lightning arrester, which comprises the following processing steps:|[0009] (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the crushed raw material is required to reach 5-10 mm;|[0010] (2) washing the crushed silicon carbide with clear water for 3-5 times, drying, sieving in a sieving machine to remove impurities, and then screening for 2-4 times in a magnetic separator;|[0011] (3) adding water into the screened silicon carbide to blend into mixed slurry with the concentration of 25-35%, adding concentrated sulfuric acid with the concentration of 98% accounting for 20-25% of the mass of the mixed slurry, stirring for 20-30 minutes, then adding sodium hydroxide, stirring while adding until the pH value of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 10-15 minutes, filtering out the silicon carbide through fractional sedimentation, and washing for 3-5 times by using clear water;|[0012] (4) and (4) placing the silicon carbide treated in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature at 750-800 ℃, naturally cooling the silicon carbide by ventilation after baking for 50-60 minutes, and then carrying out airflow flotation classification on the cooled silicon carbide.|[0013] Wherein the decarbonizer is kerosene.|[0014] The invention has the advantages and positive effects that:|[0015] the method adopts a plurality of impurity removal and refinement processes, the processed silicon carbide powder has high purity and fine granularity, the process temperature can be effectively reduced when the valve plate of the lightning arrester is produced subsequently, and the quality of the valve plate is improved.|INVENTION MODE|[0016] Detailed Description|INVENTION MODE|[0017] The first embodiment is as follows:|[0018] a treatment method of silicon carbide fine powder for lightning protection comprises the following treatment steps:|[0019] (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the crushed raw material is required to reach 5-10 mm;|[0020] (2) washing the crushed silicon carbide with clear water for 3 times, drying, sieving in a sieving machine to remove impurities, and then screening for 2 times in a magnetic separator;|[0021] (3) adding water into the screened silicon carbide to blend the silicon carbide into mixed slurry with the concentration of 25 percent, adding concentrated sulfuric acid with the concentration of 98 percent and the mass of 20 percent of the mixed slurry, stirring for 20 minutes, then adding sodium hydroxide, stirring while adding until the PH of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 10 minutes, filtering out the silicon carbide through fractional sedimentation and washing for 3 times by using clear water;|[0022] (4) and (4) placing the silicon carbide processed in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature to 750 ℃, baking for 50 minutes, ventilating and naturally cooling, and then carrying out airflow flotation classification on the cooled silicon carbide.|INVENTION MODE|[0023] The second embodiment is as follows:|[0024] a treatment method of silicon carbide fine powder for lightning protection comprises the following treatment steps:|[0025] (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the crushed raw material is required to reach 5-10 mm;|[0026] (2) washing the crushed silicon carbide with clear water for 5 times, drying, sieving in a sieving machine to remove impurities, and then putting into a magnetic separator for sieving for 4 times;|[0027] (3) adding water into the screened silicon carbide to blend into mixed slurry with the concentration of 35%, adding concentrated sulfuric acid with the concentration of 98% of the mass of the mixed slurry of 25% and stirring for 30 minutes, then adding sodium hydroxide, stirring while adding until the pH value of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 15 minutes, filtering out the silicon carbide through fractional sedimentation and washing for 5 times by using clear water;|[0028] (4) and (4) placing the silicon carbide processed in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature to be 800 ℃, baking for 60 minutes, ventilating and naturally cooling, and then carrying out airflow flotation classification on the cooled silicon carbide.|INVENTION MODE|[0029] The third concrete embodiment:|[0030] a treatment method of silicon carbide fine powder for lightning protection comprises the following treatment steps:|[0031] (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the crushed raw material is required to reach 5-10 mm;|[0032] (2) washing the crushed silicon carbide with clear water for 4 times, drying, sieving in a sieving machine to remove impurities, and then screening in a magnetic separator for 3 times;|[0033] (3) adding water into the screened silicon carbide to blend into mixed slurry with the concentration of 30%, adding concentrated sulfuric acid with the concentration of 98% and the mass of 22% of the mixed slurry, stirring for 25 minutes, then adding sodium hydroxide, stirring while adding until the pH value of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 13 minutes, filtering out the silicon carbide through fractional sedimentation, and washing for 4 times by using clear water;|[0034] (4) and (4) placing the silicon carbide processed in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature to be 780 ℃, baking for 55 minutes, ventilating and naturally cooling, and then carrying out airflow flotation classification on the cooled silicon carbide.|[0035] The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention. (CN106276907)|TECHNICAL FIELD|[0002] The invention relates to the technical field of silicon carbide material treatment, in particular to a method for treating silicon carbide fine powder for a lightning arrester.|BACKGROUND ART|[0004] The silicon carbide is prepared by smelting quartz sand, petroleum coke, wood chips and other raw materials in a resistance furnace at high temperature, and rare minerals exist in the silicon carbide in nature. Silicon carbide can be used in many fields and is a material with high demand. The valve plate is widely applied to the field of electric appliances and can play a critical role as a valve plate in a lightning protection device.|[0005] When the valve plate is made of silicon carbide, high-temperature conditions are needed, and the temperature requirements have high requirements on equipment and processes; the fineness and purity of the silicon carbide powder is an important factor in order to reduce the process temperature at the time of its preparation.|DISCLOSURE|[0006] Disclosure of Invention|[0007] The invention aims to provide a method for treating silicon carbide fine powder for a lightning arrester.|[0008] In order to realize the purpose, the invention discloses a method for processing silicon carbide fine powder for a lightning arrester, which comprises the following processing steps:|[0009] (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the crushed raw material is required to reach 5-10 mm;|[0010] (2) washing the crushed silicon carbide with clear water for 3-5 times, drying, sieving in a sieving machine to remove impurities, and then screening for 2-4 times in a magnetic separator;|[0011] (3) adding water into the screened silicon carbide to blend into mixed slurry with the concentration of 25-35%, adding concentrated sulfuric acid with the concentration of 98% accounting for 20-25% of the mass of the mixed slurry, stirring for 20-30 minutes, then adding sodium hydroxide, stirring while adding until the pH value of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 10-15 minutes, filtering out the silicon carbide through fractional sedimentation, and washing for 3-5 times by using clear water;|[0012] (4) and (4) placing the silicon carbide treated in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature at 750-800 ℃, naturally cooling the silicon carbide by ventilation after baking for 50-60 minutes, and then carrying out airflow flotation classification on the cooled silicon carbide.|[0013] Wherein the decarbonizer is kerosene.|[0014] The invention has the advantages and positive effects that:|[0015] the method adopts a plurality of impurity removal and refinement processes, the processed silicon carbide powder has high purity and fine granularity, the process temperature can be effectively reduced when the valve plate of the lightning arrester is produced subsequently, and the quality of the valve plate is improved.|INVENTION MODE|[0016] Detailed Description|INVENTION MODE|[0017] The first embodiment is as follows:|[0018] a treatment method of silicon carbide fine powder for lightning protection comprises the following treatment steps:|[0019] (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the crushed raw material is required to reach 5-10 mm;|[0020] (2) washing the crushed silicon carbide with clear water for 3 times, drying, sieving in a sieving machine to remove impurities, and then screening for 2 times in a magnetic separator;|[0021] (3) adding water into the screened silicon carbide to blend the silicon carbide into mixed slurry with the concentration of 25 percent, adding concentrated sulfuric acid with the concentration of 98 percent and the mass of 20 percent of the mixed slurry, stirring for 20 minutes, then adding sodium hydroxide, stirring while adding until the PH of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 10 minutes, filtering out the silicon carbide through fractional sedimentation and washing for 3 times by using clear water;|[0022] (4) and (4) placing the silicon carbide processed in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature to 750 ℃, baking for 50 minutes, ventilating and naturally cooling, and then carrying out airflow flotation classification on the cooled silicon carbide.|INVENTION MODE|[0023] The second embodiment is as follows:|[0024] a treatment method of silicon carbide fine powder for lightning protection comprises the following treatment steps:|[0025] (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the crushed raw material is required to reach 5-10 mm;|[0026] (2) washing the crushed silicon carbide with clear water for 5 times, drying, sieving in a sieving machine to remove impurities, and then putting into a magnetic separator for sieving for 4 times;|[0027] (3) adding water into the screened silicon carbide to blend into mixed slurry with the concentration of 35%, adding concentrated sulfuric acid with the concentration of 98% of the mass of the mixed slurry of 25% and stirring for 30 minutes, then adding sodium hydroxide, stirring while adding until the pH value of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 15 minutes, filtering out the silicon carbide through fractional sedimentation and washing for 5 times by using clear water;|[0028] (4) and (4) placing the silicon carbide processed in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature to be 800 ℃, baking for 60 minutes, ventilating and naturally cooling, and then carrying out airflow flotation classification on the cooled silicon carbide.|INVENTION MODE|[0029] The third concrete embodiment:|[0030] a treatment method of silicon carbide fine powder for lightning protection comprises the following treatment steps:|[0031] (1) carrying out primary crushing on a silicon carbide raw material by using a jaw crusher, and then putting the primary crushed raw material into a back-impact crusher for secondary crushing, wherein the crushed raw material is required to reach 5-10 mm;|[0032] (2) washing the crushed silicon carbide with clear water for 4 times, drying, sieving in a sieving machine to remove impurities, and then screening in a magnetic separator for 3 times;|[0033] (3) adding water into the screened silicon carbide to blend into mixed slurry with the concentration of 30%, adding concentrated sulfuric acid with the concentration of 98% and the mass of 22% of the mixed slurry, stirring for 25 minutes, then adding sodium hydroxide, stirring while adding until the pH value of the slurry reaches 6.8-7.1, finally adding a carbon removing agent, mixing and stirring for 13 minutes, filtering out the silicon carbide through fractional sedimentation, and washing for 4 times by using clear water;|[0034] (4) and (4) placing the silicon carbide processed in the step (3) into a heating furnace for high-temperature baking, setting the baking temperature to be 780 ℃, baking for 55 minutes, ventilating and naturally cooling, and then carrying out airflow flotation classification on the cooled silicon carbide.|[0035] The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention. Family Number|(75072744)|75072744|Abstract|(CN106276907 A)|The invention provides a treatment method of silicon carbide fine powder for a lightning arrester . The treatment method includes the treatment steps that 1, a silicon carbide raw material is preliminarily crushed through a jaw crusher , and then the material is put in an impact crusher to be secondarily crushed ; 2, after silicon carbide is washed with clear water , silicon carbide is dried and put in a screener for impurity screening - out , and silicon carbide is put in a magnetic separator to be screened ; 3, water is added , the material is blended into mixed paste , after concentrated sulfuric acid is added and stirring is carried out , sodium hydroxide is added , stirring is carried out while adding is carried out , finally , a carbon removal agent is added , after the material is mixed and stirred , silicon carbide is filtered out through classification sedimentation , and silicon carbide is washed with clear water ; 4, silicon carbide treated in the step 3 is put in a heating furnace for high - temperature baking , after silicon carbide is baked , ventilation is carried out for natural cooling , and then airflow flotation classification is carried out . The treatment method has the advantages that multiple impurity removal and refining processes are adopted , the treated silicon carbide powder is high in purity and fine in granularity , and when a lightning arrester valve block is produced in the following process , the process temperature can be effectively reduced , and the quality of the valve block is improved . |IPC codes|(CN106276907 A)|C01B - 031/36 | Materials, metallurgy C01B-031/36 C01B-031/36 CN115672541 CN115672541 103693552 WHO=Examiner SELF=N CAT=Y CN103964439|CN101804982|CN103950931 CN103964439 67163062 WHO=Examiner SELF=N CAT=Y|CN101804982 7061823 WHO=Examiner SELF=N CAT=Y|CN103950931 67118612 WHO=Examiner SELF=N CAT=A CN101804982; CN103950931; CN103964439 LAPSED (CN106276907)|LAPSED DEAD (CN106276907)|DEAD (CN106276907)|LEGAL DETAILS FOR CN106276907|Actual or expected expiration date=2018-08-28|Legal state=DEAD|Status=LAPSED|Event publication date=2016-08-23|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201610704069|Application date=2016-08-23|Standardized application number=2016CN-0704069|Event publication date=2017-01-04|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN106276907|Publication stage code=A|Publication date=2017-01-04|Standardized publication number=CN106276907|Event publication date=2017-01-04|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2017-02-01|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2018-08-28|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjlLUEJLxa38FFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=7YG5WsCeITIPbYR0t2VB95NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN106276907)|NAME=YAO KUN|NAME=YAO WANG|NAME=WANG CHUANWEN 0 1 Titre: (CN106276907)|Treatment method of silicon carbide fine powder for lightning arrester Résumé: (CN106276907)|The invention provides a treatment method of silicon carbide fine powder for a lightning arrester. The treatment method includes the treatment steps that 1, a silicon carbide raw material is preliminarily crushed through a jaw crusher, and then the material is put in an impact crusher to be secondarily crushed; 2, after silicon carbide is washed with clear water, silicon carbide is dried and put in a screener for impurity screening-out, and silicon carbide is put in a magnetic separator to be screened; 3, water is added, the material is blended into mixed paste, after concentrated sulfuric acid is added and stirring is carried out, sodium hydroxide is added, stirring is carried out while adding is carried out, finally, a carbon removal agent is added, after the material is mixed and stirred, silicon carbide is filtered out through classification sedimentation, and silicon carbide is washed with clear water; 4, silicon carbide treated in the step 3 is put in a heating furnace for high-temperature baking, after silicon carbide is baked, ventilation is carried out for natural cooling, and then airflow flotation classification is carried out. The treatment method has the advantages that multiple impurity removal and refining processes are adopted, the treated silicon carbide powder is high in purity and fine in granularity, and when a lightning arrester valve block is produced in the following process, the process temperature can be effectively reduced, and the quality of the valve block is improved. 57 Abstract gpt-4o-mini no The article focuses on a treatment method for silicon carbide fine powder used in lightning arresters, which does not relate to accelerated weathering or CO₂ capture.
65 CN202310394318 CN202310394318 CN116420457|CN116420457 105745947 CN116420457 B 2025-05-06 [CN116420457B]|CN116420457 A 2023-07-14 [CN116420457] 2023-04-13 2023-04-13 2025-05-06|2023-07-14 (CN116420457B)|2025-05-06 (CN116420457)|2043-04-13 (CN116420457)|Method for improving carbon fixation capacity of soil of loess plateau abandoned wasteland (CN116420457)|The invention relates to the technical field of carbon sequestration, and particularly discloses a method for improving the soil carbon sequestration capacity of abandoned land of loess plateau, which comprises the steps of carbon sequestration agent preparation and plant community structure adjustment. The carbon sequestration agent is prepared from biochar, crushed straw and a complex microbial inoculant according to the dosage ratio of (4-6) g: (2-3) g: (6-10) mL. The complex microbial inoculant is prepared by mixing nitrified brevibacillus vv6, nitrobacter winogradsky XY-01, authigenic nitrogen-fixing bacteria MBC5 and bradyrhizobium Qian2 according to the volume ratio of 1: 1: (2-3): (2-4); the plant community structure adjustment comprises reseeding indigenous leguminous plants and gramineous plants, and reducing the number of dominant species of compositae plants. By applying the carbon reinforcing agent and optimizing the plant community, the carbon sequestration capability of the abandoned land soil of the loess plateau can be remarkably improved, and the method has important practical significance for building a carbon sequestration and sink increasing type vegetation restoration ecological system and assists an ecological environment fragile area to achieve the dual-carbon target. NORTH WEST AGRICULTURE & FORESTRY UNIVERSITY (CN116420457)|NORTHWEST SCI-TECH UNIVERSITY OF AGRICULTURE & FORESTRY ([CN])|(CN116420457)|NORTHWEST SCI-TECH UNIVERSITY OF AGRICULTURE & FORESTRY ([CN]) ZHONG ZEKUN|WANG XING|WANG YONGLIANG|REN CHENGJIE|HAN XINHUI|YANG GAIHE (CN116420457)|ZHONG ZEKUN|WANG XING|WANG YONGLIANG|REN CHENGJIE|HAN XINHUI|YANG GAIHE|(CN116420457)|ZHONG ZEKUN|WANG XING|WANG YONGLIANG|REN CHENGJIE|HAN XINHUI|YANG GAIHE (CN116420457)|CUI RUIYING;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 61223 (CN116420457)|1. A method for improving the carbon fixation capacity of loess plateau abandoned land soil is characterized in that a carbon strengthening agent is applied to the soil, and the plant community structure is adjusted; The carbon fixing agent is prepared from biochar, straw fragments and a composite microbial agent according to the dosage ratio of 4-6g to 2-3g to 6-10 mL; The composite microbial inoculum is prepared by mixing a bacillus brevis v6 microbial inoculum, a nitrifying bacillus XY-01 microbial inoculum, an authigene nitrogen fixing bacterium MBC5 microbial inoculum and a slow rooting tumor bacterium Qian2 microbial inoculum according to the volume ratio of 1:1:2-3:2-4; the plant community structure adjustment specifically comprises the step of supplementing leguminous plants and gramineous plants, and the number of dominant species of the asteraceae plants is reduced. | (CN116420457)|In order to solve the technical problems, the invention provides a method for improving the carbon fixing capability of loess plateau abandoned land soil, which is characterized in that a carbon fixing agent is applied to the soil, and the plant community structure is adjusted to improve the carbon fixing capability of the soil.The invention provides a method for improving the carbon fixation capacity of loess plateau abandoned land soil, which comprises the steps of applying a carbon strengthening agent into the soil and adjusting plant community structures;|The invention relates to the technical field of carbon fixation, and particularly discloses a method for improving the carbon fixation capacity of loess plateau barren land soil, which comprises the steps of preparing a carbon fixation agent and adjusting a plant community structure, wherein the carbon fixation agent is prepared from biochar, straw fragments and a composite microbial agent according to the dosage ratio of 4-6g to 2-3g to 6-10mL, the composite microbial agent is prepared by mixing bacillus brevis v6, nitrifying bacillus Vietnamii XY-01, authigenic azotobacter MBC5 and slow rooting tumor Qian2 according to the volume ratio of 1:1:2-3:2-4, and the plant community structure adjustment comprises the steps of supplementing leguminous plants and gramineae plants, and reducing the number of dominant species of the asteraceae plants.|The invention relates to the technical field of carbon fixation, in particular to a method for improving the carbon fixation capacity of soil of a loess plateau abandoned land.| (CN116420457)|CARBON FIXATION(100,24)|LOESS PLATEAU(100,22)|ABANDONED LAND SOIL(100,12)|CARBON FIXATION CAPACITY(100,12)|ABANDONED WASTELAND(100,2)|LOESS PLATEAU ABANDONED WASTELAND(100,1)|SOIL CAPACITY(100,1)|MICROBIAL INOCULUM(83,26)|LOESS PLATEAU SOIL(74,10)|ASTERACEA PLANT DOMINANT SPECIES(67,7)|AUTHIGENIC AZOTOBACTER(66,1)|SUPPLEMENTING LEGUMINOUS PLANT(62,3)|NITRIFYING BACILLUS(60,5)|SLOW ROOTING TUMOR BACTERIUM(59,2)|SLOW ROOTING TUMOR(56,1)|STRAW FRAGMENT(47,5)|ASTERACEA PLANT(46,18)|LOESS PLATEAU BARREN LAND(45,1)|BARREN LAND(42,12)|GRAMINEOUS PLANT(42,10)|COMPOSITE MICROBIAL INOCULUM(41,6)|STRAIN PURIFICATION(39,11)|AUTHIGENE NITROGEN FIXING BACTERIUM(39,2)|LOESS PLATEAU ABANDONED LAND(37,2)|TUMOR BACTERIUM(36,2)|ASTRAGALUS TRIFOLITICUS(36,1)|CRYPTOCARYA PALIURUS(35,1)|NITRIFYING BACTERIUM XY 01(33,2)|XY 01 MICROBIAL INOCULUM(32,6)|BACILLUS BREVIS V(32,4)|COLLECTION INCREASING VEGETATION RESTORATION(31,1)|GRAMINEAE PLANT(29,6)|VIOLA YEDOENSIS(29,2)|SWEETGUM FRUIT(28,1)|DOSAGE RATIO(26,4)|SLOW ROOTING(26,3)|BIOCHAR(25,4)|CONYZA SATIVA(25,2)|ABANDONED LAND(24,33)|PLANT COMMUNITY(24,30)|CARBON FIXING CAPABILITY(21,7)|DOMINANT SPECIES(20,8)|SOIL CARBON FIXING CAPABILITY(19,2)|ABANDONED BARREN LAND COVERAGE(18,5)|GROUND(17,24)|PLANT COMMUNITY STRUCTURE(17,20)|ECOLOGICAL ENVIRONMENT FRAGILE AREA(17,1)|SOIL CARBON FIXATION CAPACITY(16,9)|PLATE STREAK TRANSFER(16,4)|CRYPTOSPORIDIUM(16,1)|PURIFIED BACTERIAL STRAIN(15,3)|PISUM SATIVUM(15,1)|SPANISH NEEDLE HERB(14,3)|SIGNIFICANCE(14,2)|BUILDING CARBON FIXING(14,1)|CARBON FIXING(13,18)|NITROBACTER VICKER(13,4)|ASTERACEA PLANT COVERAGE(13,3)|HERBA ARTEMISIA CAPILLARY(13,2)|HERBA CHENOPODII GRAMINEOUS PLANT(13,1)|TRIFOLITH ASTRAGALUS ROOT(12,2)|LEGUMINOSAE PLANT(11,6)|MICROBIAL BIOMASS CARBON(11,4)|BARREN LAND YEAR(11,2)|CONTINENTAL SEMIARID MONSOON CLIMATE(11,1)|HERBA MESONA CHINENSIS(11,1)|LESPEDEZA MULTIFLORA SEED(11,1)|COMPOSITAE PLANT(10,5)|VEGETATION INVESTIGATION(10,3)|YMA SOLID MEDIUM(10,3)|ASTEROID PLANT COVERAGE(10,2)|ASTRAGALUS TRIFOLIATUS(10,2)|LB SOLID MEDIUM(10,2)|DOUBLE CARBON TARGET(10,1)|HERBA CHENOPODII GRASS(10,1)|ABANDONED LAND PLANT COMMUNITY(9,4)|ABANDONED LAND COVERAGE(9,3)|GRAMINEAE COVERAGE(9,3)|LEGUMINOUS PLANT CONTRIBUTION(9,3)|VEGETATION SURVEY(9,3)|ASTRAGALUS TRIFOLITAN(9,2)|INOCULUM SIZE(9,2)|RADIX ASTRAGALUS(9,2)|VETCH(9,2)|CRYPTOPSIS SUBULATA SEED(9,1)|GRAMINEAE DENSITY(8,4)|MICROBIOLOGICAL CULTURE COLLECTION(8,4)|VOLUME RATIO(8,4)|ASTERACEA FAMILY(8,2)|CHLOROFORM FUMIGATION EXTRACTION(8,1)|DAGHESTAN ASTRAGALUS SEED(8,1)|GRAMINEOUS PLANT COMPLEMENTARY SOWING(8,1)|LOESS PLATEAU VEGETATION COVERAGE(8,1)|MESONA BLUME SEED(8,1)|PHOTO THERMAL GROUND RESOURCE(8,1)|SHIMADZU TOC INSTRUMENT(8,1)|SLOW ROOTING TUMOR FUNGUS(8,1)|SOIL MICROBIAL FLORA(8,1)|TRIFOLITH ASTRAGALUS MEMBRANACEUS(8,1)|SOIL CARBON SEQUESTRATION CAPACITY(7,4)|YMA LIQUID MEDIUM(7,2)|BARREN LAND PLANT COMMUNITY(7,1)|EOLIAN LOESS MATRIX(7,1)|RHIZOBIUM CHROMENENSIS(7,1)|RHIZOBIUM SLOWNESS(7,1)|CRYPTOTAENIA JAPONICA(6,4)|LB LIQUID MEDIUM(6,3)|PLANT POPULATION(6,2)|YANAN CITY(6,2)|ABANDONED WASTELAND SOIL(6,1)|ALTERNARIA ALTERNATA SEED(6,1)|AVERAGE ANNUAL EVAPOTRANSPIRATION(6,1)|BIDENS PARVIFLORA(6,1)|COMPOSITAE COVERAGE(6,1)|CYNANCHUM KOMAROVII(6,1)|ELYMUS CAPE GRASS(6,1)|GRAMINEE GRASS(6,1)|LOESS PLATEAU ECOLOGICAL ENVIRONMENT(6,1)|LOESS PLATEAU UNDERGROUND(6,1)|VIOLA YESSOENSIS(6,1)|GRASS SEED(5,6)|OXIDIZABLE ORGANIC CARBON(5,5)|NITROGEN FIXING BACTERIA MBC(5,3)|PHOTOSYNTHESIS CARBON FIXATION(5,2)|SLOW RHIZOBIA(5,2)|SOIL PARTICLE(5,2)|SOIL SAMPLE FUMIGATION(5,2)|SOLID FLAT PLATE(5,2)|ABANDONED LAND ECONOMIC BENEFIT(5,1)|AUTHIGENIC NITROGEN FIXING BACTERIUM(5,1)|AVERAGE ANNUAL RAINFALL(5,1)|COLUMNAR BLADE(5,1)|FARMLAND MANAGEMENT(5,1)|FERTILIZER CONSERVATION(5,1)|GRASS CONTRIBUTION(5,1)|GRASS COVERAGE(5,1)|LOESS PLATEAU LAND(5,1)|LOESS PLATEAU PIONEER SPECIES(5,1)|MICROORGANISM CARBON PROMOTION(5,1)|PISUM ALBUM(5,1)|PLANT COMMUNITY SPECIES UNIFORMITY(5,1)|SOIL FUMIGATION(5,1)|SOIL MICROORGANISM(5,1)|YELLOW COTTON SOIL(5,1)|PLANT SPECIES(4,9)|INERT ORGANIC CARBON CONTENT(4,8)|SOIL ORGANIC CARBON RESERVE(4,7)|SIEVE(4,5)|PRESERVATION(4,4)|SOLID PLATE(4,4)|DESICCATOR(4,3)|SOIL CARBON FIXING CAPACITY(4,3)|DENSITY CONTRIBUTION(4,2)|ECOLOGICAL SYSTEM(4,2)|MICROBIAL CARBON CONTENT(4,2)|UNFUSED SOIL SAMPLE(4,2)|ABANDONED LAND ABILITY(4,1)|ABANDONED LAND IMPORTANCE(4,1)|ARTIFICIAL INTERFERENCE(4,1)|BACTERIAL STRAIN MBC(4,1)|BEAN GRASS MIXED SOWING(4,1)|COMPOSITAE DOMINANT SPECIES REMOVAL(4,1)|CONSUMED POTASSIUM PERMANGANATE(4,1)|COVERAGE CONTRIBUTION(4,1)|CRYPT SEED GRASS(4,1)|ECOLOGICAL ENVIRONMENT QUALITY(4,1)|ECOLOGICAL PROTECTION(4,1)|ENHANCEMENT CAPABILITY(4,1)|EXPERIMENTAL PLOT(4,1)|FREE LIVING AZOTOBACTER MBC(4,1)|GRASS DENSITY(4,1)|LEGUMINOUS PLANT MIXED SOWING(4,1)|LEGUMINOUS PLANT NATIVE(4,1)|LOESS PLATEAU FARMLAND AREA(4,1)|LOOSE SOIL TEXTURE(4,1)|MICROBIAL NITROGEN FIXING FLORA(4,1)|MICROORGANISM FUNCTION(4,1)|MIXED SOWING PROPORTION(4,1)|NEGATIVE ECOLOGICAL INFLUENCE(4,1)|NITROGEN BIOCHAR CARBON ADSORPTION(4,1)|NONFUMIGATED SOIL SAMPLE(4,1)|PASTURE YIELD(4,1)|PENTAGULF STREAM(4,1)|PETRI DISH(4,1)|PLANT COMMUNITY REGULAR ADJUSTMENT(4,1)|PLANT COMMUNITY SUCCESSION(4,1)|POROUS BIOCHAR(4,1)|PORTABLE REFRIGERATOR(4,1)|RAINFALL ACCOUNT(4,1)|SHORT BACILLUS NITRIFICATION(4,1)|SLOW GROWING RHIZOBIUM(4,1)|SLOW RHIZOBIUM(4,1)|SODIUM HEXAMETAPHOSPHATE EXTRACTION(4,1)|SOIL CARBON RESERVOIR CAPACITY(4,1)|SOIL CARBON SEQUESTRATION DEPENDANCE(4,1)|TEMPERATE ZONE MODERATION(4,1)|UNDERGROUND SOIL CARBON ACCUMULATION(4,1)|VEGETATION GROWTH VIGOROUS PERIOD(4,1)|VEGETATION NATURAL SUCCESSION(4,1)|YEAST JUICE(4,1)|YELLOW RIVER BASIN(4,1)|BEAKER(3,5)|AGAR(3,4)|SOIL VOLUME WEIGHT(3,4)|TREND(3,4)|DISTRICT(3,2)|FLAT STREAK TRANSFER(3,2)|LEGUME(3,2)|MIXED MODE(3,2)|SOIL SAMPLE COLLECTION(3,2)|SPECIES RICHNESS(3,2)|STRAW(3,2)|SUPERNATANT(3,2)|ADAPTABILITY(3,1)|ANSAI AREA ECOLOGICAL RESTORATION(3,1)|BATTLEFIELD(3,1)|CARBON RESERVOIR STABILITY(3,1)|CARBON SEQUESTRATION INFLUENCE(3,1)|DIGESTION TUBE(3,1)|EROSION RESISTANCE(3,1)|EXERTION(3,1)|FALLEN MATTER(3,1)|FRAGILE ZONE(3,1)|GROWTH ENVIRONMENT(3,1)|HYDROCHLORIC ACID DIGESTION(3,1)|LOESS PLATEAU ABDOMEN AREA(3,1)|LOESS PLATEAU CARBON SINK(3,1)|MBC CONTENT(3,1)|PALATABILITY(3,1)|PERMANGANATE OXIDATIVE ORGANIC CARBON(3,1)|PLANT COMMUNITY ADJUSTMENT(3,1)|PLANT COMMUNITY DENSITY(3,1)|PLANT PHOTOSYNTHETIC CARBON FIXATION(3,1)|POC CONTENT(3,1)|POXC CONTENT(3,1)|PREPARED BACILLUS BREVIS(3,1)|REGIONAL ATMOSPHERIC CARBON DIOXIDE(3,1)|REGULATION(3,1)|REINFORCING CARBON(3,1)|ROC CONTENT(3,1)|ROW SPACING(3,1)|SETARIA ITALICA(3,1)|SOIL CARBON SEQUESTRATION ABILITY(3,1)|SOIL INCREASED YEAR(3,1)|SOIL NITROGEN FIXING(3,1)|SOIL SAMPLE DIGESTION(3,1)|TEST COMMUNITY(3,1)|TEST ZONE OVERVIEW(3,1)|TOTAL SOWING(3,1)|WULI GULF REGION(3,1)|STANDARD ERROR(2,13)|SULFURIC ACID EXTERNAL(2,3)|ABSORBANCE(2,1)|ACTIVATION CULTURE MEDIUM(2,1)|ALTITUDE(2,1)|AVAILABLE BIOCHAR(2,1)|AVERAGE INDEX(2,1)|CARBON FIXATION CAPACITY MEASUREMENT(2,1)|CARBON LOSS RISK(2,1)|CLEANED SOIL SAMPLE(2,1)|CRYPTOCARYA(2,1)|CULTIVATION(2,1)|CULTURE MEDIUM ACTIVATION(2,1)||(CN116420457)|LOESS PLATEAU(100,25)|CARBON FIXATION(100,23)|ABANDONED LAND SOIL(100,19)|CARBON FIXATION CAPACITY(100,11)|ABANDONED WASTELAND(100,2)|LOESS PLATEAU ABANDONED WASTELAND(100,1)|SOIL CAPACITY(100,1)|VILLAGE GRAMINEOUS PLANT(87,1)|SLOW ROOTING TUMOR BACTERIUM(85,4)|MICROBIAL INOCULUM(79,24)|ROOTING TUMOR BACTERIUM(78,1)|ASTERACEA PLANT DOMINANT SPECIES(67,7)|COMPOSITE MICROBIAL INOCULUM(63,7)|LOESS PLATEAU SOIL(60,6)|GRAMINEOUS PLANT(54,11)|HERBA MESONA CHINENSIS(48,2)|STRAW FRAGMENT(47,5)|ASTERACEA PLANT(46,20)|NITRIFYING BACILLUS(40,3)|AUTHIGENE NITROGEN FIXING BACTERIUM(39,2)|SUPPLEMENTING LEGUMINOUS PLANT(39,2)|TRIFOLITH ASTRAGALUS ROOT(38,3)|ASTRAGALUS TRIFOLITICUS(36,1)|STRAIN PURIFICATION(33,12)|XY 01 MICROBIAL INOCULUM(33,4)|LOESS PLATEAU ABANDONED LAND(33,3)|BACILLUS BREVIS V(32,4)|TUMOR BACTERIUM(32,3)|COLLECTION INCREASING VEGETATION RESTORATION(31,1)|NITRIFYING BACTERIUM(29,6)|PLANT COMMUNITY(26,30)|DOSAGE RATIO(26,4)|SLOW ROOTING(26,3)|CONYZA SATIVA(25,2)|ABANDONED LAND(24,37)|NITROGEN FIXING BACTERIA MBC(24,6)|BIOCHAR(23,5)|LEGUMINOUS PLANT(22,33)|CARBON FIXING CAPABILITY(21,7)|DOMINANT SPECIES(20,9)|HERBA ARTEMISIA CAPILLARY(19,4)|SOIL CARBON FIXING CAPABILITY(19,2)|SPANISH NEEDLE HERB(18,5)|GROUND(17,29)|ECOLOGICAL ENVIRONMENT FRAGILE AREA(17,1)|CARBON FIXING(16,18)|COMPOSITAE PLANT(16,11)|SOIL CARBON FIXATION CAPACITY(16,8)|SLOW GROWING RHIZOBIA(16,3)|HERBA ARTEMISIA ARGYI(16,2)|CRYPTOSPORIDIUM(16,1)|NITROGEN FIXING BACTERIA(15,9)|ASTERACEA PLANT COVERAGE(15,4)|PLANT COMMUNITY STRUCTURE(14,19)|GRAMINEAE PLANT(14,11)|CRYPTOTAENIA JAPONICA(14,3)|SIGNIFICANCE(14,2)|BUILDING CARBON FIXING(14,1)|ASTRAGALUS TRIFOLITAN(13,4)|VEGETATION INVESTIGATION(12,4)|ABANDONED LAND COVERAGE(11,4)|ASTERACEA FAMILY(11,4)|FLAT STREAK TRANSFER(11,3)|NITROBACTER VICKER(11,3)|ABANDONED BARREN LAND COVERAGE(11,2)|CONTINENTAL SEMIARID MONSOON CLIMATE(11,1)|LESPEDEZA MULTIFLORA SEED(11,1)|COMMUNITY DENSITY(10,10)|PLATE STREAK TRANSFER(10,3)|YMA LIQUID CULTURE(10,3)|YMA SOLID CULTURE MEDIUM(10,3)|ASTEROID PLANT COVERAGE(10,2)|LEGUMINOUS PLANT TREMENDOUS AMPLIFICATION(10,2)|RHIZOBIUM CHROMENENSIS(10,2)|DOUBLE CARBON TARGET(10,1)|SOIL CARBON SEQUESTRATION CAPACITY(9,7)|ABANDONED LAND PLANT COMMUNITY(9,4)|LB SOLID MEDIUM(9,4)|GRAMINEAE COVERAGE(9,3)|VEGETATION SURVEY(9,3)|ELYMUS CHINENSIS(9,2)|CRYPTOPSIS SUBULATA SEED(9,1)|VOLUME RATIO(8,4)|LEGUMINOSAE PLANT(8,3)|ANNUAL TREND(8,2)|FAMILY VISCUM ALBUM(8,2)|GRASS COVERAGE(8,2)|VETCH LEGUMINOUS PLANT(8,2)|CHLOROFORM FUMIGATION EXTRACTION(8,1)|DAGHESTAN ASTRAGALUS SEED(8,1)|GRAMINEOUS PLANT COMPLEMENTARY SOWING(8,1)|LOESS PLATEAU VEGETATION COVERAGE(8,1)|MESONA BLUME SEED(8,1)|PHOTO THERMAL GROUND RESOURCE(8,1)|SHIMADZU TOC INSTRUMENT(8,1)|SOIL MICROBIAL FLORA(8,1)|TRIFOLITH ASTRAGALUS MEMBRANACEUS(8,1)|SOLID PLATE(7,6)|BARREN LAND PLANT COMMUNITY(7,1)|EOLIAN LOESS MATRIX(7,1)|LB LIQUID MEDIUM(6,4)|COVERAGE CONTRIBUTION(6,2)|PLANT COMMUNITY COVERAGE(6,2)|PLANT POPULATION(6,2)|YANAN CITY(6,2)|ABANDONED WASTELAND SOIL(6,1)|ALTERNARIA ALTERNATA SEED(6,1)|AVERAGE ANNUAL EVAPOTRANSPIRATION(6,1)|BIDENS PARVIFLORA(6,1)|CYNANCHUM KOMAROVII(6,1)|ELYMUS CAPE GRASS(6,1)|GRAMINEE GRASS(6,1)|LOESS PLATEAU ECOLOGICAL ENVIRONMENT(6,1)|LOESS PLATEAU UNDERGROUND(6,1)|VIOLA YEDOENSIS(6,1)|VIOLA YESSOENSIS(6,1)|GRASS SEED(5,5)|SOIL PARTICLE(5,2)|SOIL SAMPLE FUMIGATION(5,2)|ABANDONED LAND ECONOMIC BENEFIT(5,1)|AVERAGE ANNUAL RAINFALL(5,1)|COLUMNAR BLADE(5,1)|FERTILIZER CONSERVATION(5,1)|GRAMINEAE AMPLIFICATION(5,1)|GRASS CONTRIBUTION(5,1)|LEGUMINOSAE FAMILY(5,1)|LOESS PLATEAU LAND(5,1)|LOESS PLATEAU PIONEER SPECIES(5,1)|MICROORGANISM CARBON PROMOTION(5,1)|PLANT COMMUNITY SPECIES UNIFORMITY(5,1)|SETARIA ETICA(5,1)|SOIL MICROORGANISM(5,1)|WULI GULF STREAM DOMAIN(5,1)|YELLOW COTTON SOIL(5,1)|PLANT SPECIES(4,9)|INERT ORGANIC CARBON CONTENT(4,8)|SOIL ORGANIC CARBON RESERVE(4,8)|BEAKER(4,6)|SIEVE(4,5)|FARMLAND(4,4)|LEGUME(4,4)|OXIDIZABLE ORGANIC CARBON(4,4)|FIELD PEA(4,3)|GOOSE GRASS(4,3)|DENSITY CONTRIBUTION(4,2)|ECOLOGICAL SYSTEM(4,2)|MICROBIOLOGICAL CULTURE COLLECTION(4,2)|REINFORCING CARBON(4,2)|UNFUSED SOIL SAMPLE(4,2)|ABANDONED LAND ABILITY(4,1)|ABANDONED LAND IMPORTANCE(4,1)|ARTIFICIAL INTERFERENCE(4,1)|BEAN GRASS MIXED SOWING(4,1)|COMPOSITAE DOMINANT SPECIES REMOVAL(4,1)|COMPOSITAE FAMILY(4,1)|CONSUMED POTASSIUM PERMANGANATE(4,1)|CRYPT SEED GRASS(4,1)|DOMINANT SPECIES ECOLOGICAL NICHE(4,1)|ECOLOGICAL ENVIRONMENT QUALITY(4,1)|ECOLOGICAL PROTECTION(4,1)|ENHANCEMENT CAPABILITY(4,1)|EXPERIMENTAL PLOT(4,1)|FIXING CARBON(4,1)|FREE LIVING AZOTOBACTER MBC(4,1)|GRAMINEAE DENSITY(4,1)|GRAMINEAE FAMILY(4,1)|GRASS DENSITY(4,1)|HERBACEOUS PLANT SEED(4,1)|LEGUMINOUS PLANT MIXED SOWING(4,1)|LEGUMINOUS PLANT NATIVE(4,1)|LOESS HILLY GULLY AREA(4,1)|LOOSE SOIL TEXTURE(4,1)|MICROBIAL BIOMASS CARBON CONTENT(4,1)|MICROBIAL NITROGEN FIXING FLORA(4,1)|MICROORGANISM FUNCTION(4,1)|MICROORGANISM STRAIN COLLECTION(4,1)|MIXED SOWING PROPORTION(4,1)|NEGATIVE ECOLOGICAL INFLUENCE(4,1)|NITROGEN BIOCHAR CARBON ADSORPTION(4,1)|NONFUMIGATED SOIL SAMPLE(4,1)|PASTURE YIELD(4,1)|PETRI DISH(4,1)|PLANT COMMUNITY REGULAR ADJUSTMENT(4,1)|PLANT COMMUNITY SUCCESSION(4,1)|PLANT DIVERSITY(4,1)|POROUS BIOCHAR(4,1)|PORTABLE REFRIGERATOR(4,1)|RAINFALL ACCOUNT(4,1)|SODIUM HEXAMETAPHOSPHATE EXTRACTION(4,1)|SOIL CARBON ACCUMULATION(4,1)|SOIL CARBON RESERVOIR CAPACITY(4,1)|SOIL CARBON SEQUESTRATION DEPENDANCE(4,1)|SOIL CARBON SEQUESTRATION ENHANCING(4,1)|SOIL MICROFLORA(4,1)|TALL PLANT(4,1)|TEMPERATE ZONE MODERATION(4,1)|UNDERGROUND SOIL(4,1)|VEGETATION GROWTH VIGOROUS PERIOD(4,1)|VEGETATION NATURAL SUCCESSION(4,1)|YEAST JUICE(4,1)|YELLOW RIVER BASIN(4,1)|YMA BROTH(4,1)|AGAR(3,4)|THREE CONTRIBUTION(3,4)|DESICCATOR(3,2)|IRRIGATION(3,2)|PLANT COLONY STRUCTURE(3,2)|PRESERVATION(3,2)|SOIL SAMPLE COLLECTION(3,2)|SPECIES RICHNESS(3,2)|STRAW(3,2)|SUPERNATANT(3,2)|ADAPTABILITY(3,1)|ALLELOCHEMICAL(3,1)|AMPLIFICATION AVERAGE(3,1)|ANSAI AREA ECOLOGICAL RESTORATION(3,1)|AVERAGE AMPLIFICATION(3,1)|BATTLEFIELD(3,1)|CARBON RESERVOIR STABILITY(3,1)|CARBON SEQUESTRATION INFLUENCE(3,1)|DIGESTION TUBE(3,1)|EROSION RESISTANCE(3,1)|EXERTION(3,1)|FALLEN MATTER(3,1)|FRAGILE ZONE(3,1)|GROWTH ENVIRONMENT(3,1)|HYDROCHLORIC ACID DIGESTION(3,1)|LOESS PLATEAU ABDOMEN AREA(3,1)|LOESS PLATEAU CARBON SINK(3,1)|MBC CONTENT(3,1)|MESONA CHINENSIS(3,1)|MICROBIAL CARBON CONTENT(3,1)|NITRIFICATION(3,1)|PALATABILITY(3,1)|PERMANGANATE OXIDATIVE ORGANIC CARBON(3,1)|PLANT COMMUNITY ADJUSTMENT(3,1)|PLANT PHOTOSYNTHETIC CARBON FIXATION(3,1)|POC CONTENT(3,1)|POXC CONTENT(3,1)|PREPARED BACILLUS BREVIS(3,1)|REGIONAL ATMOSPHERIC CARBON DIOXIDE(3,1)|REGULATION(3,1)|RING CUTTER(3,1)|ROW SPACING(3,1)|SOIL CARBON FIXATION CAPABILITY(3,1)|SOIL CARBON SEQUESTRATION ABILITY(3,1)|SOIL NITROGEN FIXING(3,1)|SOIL SAMPLE DIGESTION(3,1)|TEST COMMUNITY(3,1)|TEST ZONE OVERVIEW(3,1)|TOTAL SOWING(3,1)|UNDISTURBED SOIL SAMPLE(3,1)|STANDARD ERROR(2,13)|SULFURIC ACID EXTERNAL(2,3)|SHAKER(2,2)|ABSORBANCE(2,1)|ACCOUNTING(2,1)|ACTIVATION CULTURE MEDIUM(2,1)|ALTITUDE(2,1)|AVAILABLE BIOCHAR(2,1)|BREVIBACILLUS(2,1)|CARBON FIXATION CAPACITY MEASUREMENT(2,1)| (CN116420457)|1. A method for improving the carbon fixation capacity of loess plateau abandoned land soil is characterized in that a carbon strengthening agent is applied to the soil, and the plant community structure is adjusted;| The carbon fixing agent is prepared from biochar, straw fragments and a composite microbial agent according to the dosage ratio of 4-6g to 2-3g to 6-10 mL; | The composite microbial inoculum is prepared by mixing a bacillus brevis v6 microbial inoculum, a nitrifying bacillus XY-01 microbial inoculum, an authigene nitrogen fixing bacterium MBC5 microbial inoculum and a slow rooting tumor bacterium Qian2 microbial inoculum according to the volume ratio of 1:1:2-3:2-4; | the plant community structure adjustment specifically comprises the step of supplementing leguminous plants and gramineous plants, and the number of dominant species of the asteraceae plants is reduced. |2. The method for improving the carbon sequestration capacity of loess plateau soil according to claim 1, wherein the preparation process of the bacillus brevis v6 microbial inoculum is that the strain v6 is inoculated on an LB solid medium for activation, the purified strain is subjected to 3-4 times of plate streak transfer, the purified strain is inoculated in an LB liquid medium according to the inoculum size of 1.5%, and the bacillus brevis v6 microbial inoculum is obtained after culturing for 4 days at 28 ℃.|3. The method for improving the carbon sequestration capacity of loess plateau soil according to claim 2, wherein the preparation process of the nitrifying bacteria XY-01 agent is that the strain XY-01 is inoculated on an HA solid culture medium for activation, the purified strain is subjected to 3-4 times of plate streak transfer, 1.5% of the purified strain is inoculated on the HA liquid culture medium according to the inoculum size, and the culture is carried out for 3 days at 28 ℃ to obtain the nitrifying bacteria XY-01 agent.|4. The method for improving the carbon sequestration capacity of loess plateau soil according to claim 3, wherein the preparation process of the free-standing nitrogen fixing bacteria MBC5 microbial inoculum is that bacterial strain MBC5 is inoculated on a GD solid culture medium for activation, the purification is carried out by transferring 3-4 times on a solid flat plate, the purified bacterial strain is inoculated in GD liquid culture medium according to the inoculum size of 1.5%, and the free-standing nitrogen fixing bacteria MBC5 microbial inoculum is obtained after culturing for 3 days at 28 ℃.|5. The method for improving the carbon sequestration capacity of loess plateau soil according to claim 4, wherein the preparation process of the slow-yielding rhizobia Qian2 microbial inoculum is that the strain Qian2 is inoculated on YMA solid medium for activation, the purification is carried out by transferring 3-4 times on a solid plate, the purified strain is inoculated in YMA liquid medium according to the inoculum size of 1.5%, and the slow-yielding rhizobia Qian2 microbial inoculum is obtained after culturing for 5 days at 28 ℃.|6. The method for improving the carbon sequestration capacity of the soil of a loess plateau as recited in claim 1, wherein the carbon sequestration agent is applied in an amount of 5-10 kg/mu.|7. A method for improving the carbon sequestration of loess plateau soil as claimed in claim 1, wherein said leguminous plants include lespedeza multiflora, astragalus trifoliticus and vetch.|8. A method for improving the carbon sequestration of loess plateau soil as recited in claim 7, characterized in that said gramineous plants include mesona blume, cryptosporidium and conyza sativa.|9. The method for improving the carbon sequestration capacity of loess plateau soil as recited in claim 8, characterized in that the dominant species of the asteraceae plants are mainly sticktight, artemisia annua and artemisia capillaris.|10. The method for improving the carbon sequestration capacity of loess plateau barren lands according to claim 9, wherein the leguminous plants and the gramineous plants are planted in a mixed mode, and the seeding amounts of the Lespedeza multiflora, the Daghestan sweetgum fruit, the Viola yedoensis, the Pisum sativum, the Cynanchum otophyllum, the Cryptocarya paliurus and the Alkalaria are respectively 0.835 kg/mu, 0.415 kg/mu, 0.25 kg/mu and 0.335 kg/mu. (CN116420457)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of carbon fixation, in particular to a method for improving the carbon fixation capacity of soil of a loess plateau abandoned land.|BACKGROUND ART|[0002] The loess plateau ecological environment fragile zone and the climate change sensitive area are one of main battlefields for ecological protection and high-quality development of yellow river basin. The coverage of loess plateau vegetation is improved from 31.6% in 1999 to 62.8% in 2018, soil erosion is effectively controlled, ecological environment quality is obviously improved, and regional carbon sink function is obviously improved. The area of the loess plateau farmland is 5.7 multiplied by 10 6hm2, which accounts for 10.4 percent of the total area of grasslands in the area, the organic carbon sequestration potential of the soil on the surface layer of the loess plateau can reach 8.3t/hm 2, and the method plays an important role in the loess plateau and even the carbon budget of China. However, the carbon fixation rate of the soil of the abandoned land is slow, and the effective exertion of the carbon sink function of the ecological system is severely restricted. The reason for this is the dependence of soil carbon sequestration on functional microorganisms and plant functional groups. For example, biochar Shi Junfei can raise the carbon storage of the abandoned land soil by 10.62% within 30 days. In addition, the dominant plant functional group species in the later period of the back-up succession of the primary period of the back-up period can increase the carbon fixation rate of the soil by 200%. In view of the importance of the abandoned land in maintaining the functions of loess plateau carbon sink, the improvement of the soil carbon fixation capacity of the abandoned land is of great significance in reducing the regional atmospheric carbon dioxide concentration, reducing the greenhouse effect and the negative ecological influence thereof.|[0003] An Ansai area belongs to Yanan city of Shanxi province, and is in loess plateau abdomen area, fragile in ecological environment, serious in water and soil loss and extremely low in carbon content in soil. At present, ecological restoration of Ansai areas is mainly carried out on low-yield farmlands, namely, degraded lands are restored by natural succession of vegetation after the lands. However, long-term abandoned lands have slow effects in restoring soil structures, improving soil nutrient levels, improving soil microbial systems and the like, and the succession of plant communities on the land has extremely large uncertainty, so that the soil carbon fixation effect of the abandoned lands is not obvious, and even the carbon reserves of the abandoned lands after 30 years of abandoned lands have a trend of reduction. Therefore, the improvement of the carbon sequestration and sink enhancement capability of the abandoned land soil through manual intervention is particularly important.|DISCLOSURE|Disclosure of Invention|[0004] In order to solve the technical problems, the invention provides a method for improving the carbon fixing capability of loess plateau abandoned land soil, which is characterized in that a carbon fixing agent is applied to the soil, and the plant community structure is adjusted to improve the carbon fixing capability of the soil.|[0005] The invention provides a method for improving the carbon fixation capacity of loess plateau abandoned land soil, which comprises the steps of applying a carbon strengthening agent into the soil and adjusting plant community structures;|[0006] The carbon fixing agent is prepared from biochar, straw fragments and a composite microbial agent according to the dosage ratio of 4-6g to 2-3g to 6-10 mL; |[0007] The composite microbial inoculum is prepared by mixing a bacillus brevis v6 microbial inoculum, a nitrifying bacillus XY-01 microbial inoculum, an authigene nitrogen fixing bacterium MBC5 microbial inoculum and a slow rooting tumor bacterium Qian2 microbial inoculum according to the volume ratio of 1:1:2-3:2-4; |[0008] the plant community structure adjustment specifically comprises the step of supplementing leguminous plants and gramineous plants, and the number of dominant species of the asteraceae plants is reduced. |[0009] Further, the preparation process of the bacillus brevis v6 microbial inoculum comprises the steps of inoculating a strain v6 to an LB solid culture medium for activation, carrying out purification through 3-4 times of flat streak transfer, inoculating the purified strain into an LB liquid culture medium according to the inoculum size of 1.5%, and culturing for 4 days at 28 ℃ to obtain the bacillus brevis v6 microbial inoculum.|[0010] Further, the preparation process of the Nitrobacter vickers XY-01 microbial inoculum comprises the steps of inoculating a bacterial strain XY-01 to an HA solid culture medium for activation, carrying out purification through 3-4 times of plate streak transfer, inoculating the purified bacterial strain into the HA liquid culture medium according to the inoculum size of 1.5%, and culturing for 3 days at the temperature of 28 ℃ to obtain the Nitrobacter vickers XY-01 microbial inoculum.|[0011] The preparation process of the free-living nitrogen fixing bacteria MBC5 microbial inoculum comprises the steps of inoculating bacterial strain MBC5 to a GD solid culture medium for activation, transferring the bacterial strain onto a solid flat plate for 3-4 times for purification, inoculating the purified bacterial strain into a GD liquid culture medium according to the inoculation amount of 1.5%, and culturing for 3 days at 28 ℃ to obtain the free-living nitrogen fixing bacteria MBC5 microbial inoculum.|[0012] Further, the preparation process of the slow rhizobia Qian2 microbial inoculum comprises the steps of inoculating the strain Qian2 onto YMA solid medium for activation, carrying out purification by transferring on a solid plate for 3-4 times, inoculating the purified strain into YMA liquid medium according to the inoculum size of 1.5%, and culturing at 28 ℃ for 5 days to obtain the slow rhizobia Qian2 microbial inoculum.|[0013] Further, the application amount of the carbon fixing agent is 5-10 kg/mu.|[0014] The plant community structure adjustment specifically comprises the step of supplementing and sowing the leguminous plants and the gramineous plants in the soil, so that the number of dominant species of the asteraceae plants is reduced.|[0015] Further, the leguminous plants include Lespedeza multiflora, astragalus trifolitan and Viola yedoensis.|[0016] Further, the gramineous plants include mesona blume, cryptotaenia japonica and conyza sativa.|[0017] Further, the dominant species of the Compositae plant mainly comprise Bidens parviflora, artemisia annua and Artemisia capillaris.|[0018] Further, the leguminous plants and the gramineous plants are mixed-sown;|[0019] the seeding amount of the Lespedeza multiflora, the trifolith astragalus root, the field peas, the herba mesonae chinensis, the cryptotaenia japonica and the elymus cape is respectively 0.835 kg/mu, 0.415 kg/mu, 0.25 kg/mu and 0.335 kg/mu. |[0020] Compared with the prior art, the invention has the beneficial effects that:|[0021] 1. According to the invention, the carbon fixing agent formed by compounding the biochar, the straw fragments and the composite microbial inoculum is applied to the soil, on one hand, the soil carbon fixing is increased while the soil nitrogen fixing effect and the nitrification effect are promoted through reconstruction of the microbial nitrogen fixing flora, and the growth environment of plant root systems can be improved and the root system development is accelerated through improvement of the microbial flora of the soil, so that the aim of increasing the underground soil carbon accumulation is achieved. On the other hand, porous biochar can adsorb a large amount of carbon components, improve the carbon reservoir capacity of soil and increase the carbon reservoir stability. |[0022] 2. The invention relates to a method for preparing a plant with high photosynthetic carbon fixation efficiency, which comprises the steps of taking a asteraceae plant as a pioneer species of loess plateau, evolving unique physiological morphological characteristics in the process of adapting to drought and barren, such as scale-shaped, strip-shaped, columnar or needle-shaped blades which are beneficial to water conservation, but also causing the photosynthesis carbon fixation efficiency of the unit leaf area of the asteraceae plant to be low, capturing a large amount of photothermal soil resources by a large plant and developed root system of the asteraceae plant, and influencing the photosynthesis carbon fixation of other short plants;|[0023] 3. The invention can increase the overground vegetation coverage, plant diversity and species richness by reducing the number of dominant species of the asteraceae plants, reduce the carbon loss risk caused by soil erosion and play a role in soil conservation, water conservation, fertilizer conservation and carbon fixation; |[0024] 4. the feeding value of the asteraceae plants is generally lower than that of grasses of graminees and leguminous plants, and the native leguminous plants and the grasses of the invention have strong adaptability and high survival rate, can increase the yield of pastures with better palatability, and improve the economic benefit of abandoned lands; |[0025] 5. The method provided by the invention can realize the linkage effect of 'plant photosynthetic carbon fixation-microorganism carbon promotion by nitrogen-biochar carbon adsorption' by applying the carbon strengthening agent and adjusting the plant community structure, increases the combined carbon fixation effect of the soil on the land and the underground of the loess plateau, cooperatively improves the carbon fixation capacity, the carbon warehouse reserves and the carbon warehouse stability of the soil, is natural and environment-friendly, has strong operability, is easy to realize and popularize, can rapidly, effectively and continuously improve the carbon fixation capacity of the soil, and can be suitable for the land of the loess plateau and other types of grasslands. |INVENTION MODE|Detailed Description|[0026] The following detailed description of specific embodiments of the invention is, but it should be understood that the invention is not limited to specific embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. The experimental methods described in the examples of the present invention are conventional methods unless otherwise specified, and materials, reagents, etc. used in the examples described below are commercially available.|[0027] Example 1|[0028] The embodiment provides a method for improving the carbon fixation capacity of soil of a loess plateau abandoned land.|[0029] 1. Experimental materials|[0030] 1. Material source|[0031] The biochar used in the invention is commercially available biochar;|[0032] The straw scraps used in the invention are obtained by crushing commercial straw; |[0033] The nitrifying short bacillus v6 is purchased from the China general microbiological culture collection center with the preservation number GDMCC NO:60296, the nitrifying bacillus XY-01 is purchased from the China general microbiological culture collection center with the preservation number CGMCC No.10171, the authigenic nitrogen fixing bacterium MBC5 is purchased from the China general microbiological culture collection center with the preservation number CGMCC No.10821, and the slow-growing rhizobium Qian2 is purchased from the China general microbiological culture collection center with the preservation number GDMCC NO:61612. |[0034] 2. Preparation of the culture Medium|[0035] Bacillus brevis v6 activating culture medium (LB liquid medium) comprising tryptone 10g, yeast extract 5g, sodium chloride 10g, distilled water 1000mL, and additional 18g agar for LB solid culture medium;|[0036] The Nitrobacter vickers XY-01 activation medium (HA liquid medium) comprises 2.55g of sodium dihydrogen phosphate, 0.27g of potassium dihydrogen phosphate, l.5g of sodium nitrite, 0.03g of magnesium sulfate, 0.01g of calcium chloride, 0.3g of sodium chloride, 0.03g of ferrous sulfate and 1000mL of distilled water, wherein 18g of agar is additionally added into the HA solid medium; |[0037] the free-living nitrogen fixing bacteria MBC5 activation culture medium (GD liquid culture medium) comprises 0.2g of monopotassium phosphate, 0.2g of magnesium sulfate, 0.2g of sodium chloride, 5g of calcium carbonate, 10g of mannitol, 0.1g of calcium sulfate and 1000mL of distilled water, wherein 20g of agar is additionally added into the GD solid culture medium; |[0038] The active culture medium (YMA liquid culture medium) of the rhizobium slowness Qian2 comprises 0.5g of dipotassium hydrogen phosphate, 0.2g of sodium chloride, 0.2g of magnesium sulfate heptahydrate, 0.1g of calcium sulfate, 1g of calcium carbonate, 0.001g of vitamin B, 100mL of yeast juice, 10g of mannitol and distilled water to 1000mL, wherein 18g of agar is additionally added into the YMA solid culture medium. |[0039] 2. Preparation of soil carbon fixing agent|[0040] 1. Preparation of composite microbial inoculum|[0041] (1) Preparation of bacillus brevis v6 microbial inoculum|[0042] Inoculating the strain v6 to an LB solid medium for activation, carrying out purification through 3-4 times of plate streak transfer, inoculating the purified strain into an LB liquid medium according to the inoculum size of 1.5%, and culturing for 4 days at 28 ℃ to obtain the bacillus brevis v6 microbial inoculum.|[0043] (2) Preparation of Nitrobacter vickers XY-01 microbial inoculum|[0044] The strain XY-01 is inoculated on an HA solid culture medium for activation, the purification is carried out through 3-4 times of flat streak transfer, the purified strain is inoculated into an HA liquid culture medium according to the inoculum size of 1.5 percent, and the culture is carried out for 3 days at the temperature of 28 ℃ to obtain the nitrifying bacteria XY-01.|[0045] (3) Preparation of free-living azotobacter MBC5 microbial inoculum|[0046] The strain MBC5 is inoculated on a GD solid culture medium for activation, the purification is carried out by transferring on a solid plate for 3-4 times, the purified strain is inoculated on a GD liquid culture medium according to the inoculum size of 1.5 percent, and the strain is cultured for 3 days at 28 ℃ to obtain the free-living nitrogen-fixing bacteria MBC5 microbial inoculum.|[0047] (4) Preparation of Rhizobium chromenensis Qian2 microbial inoculum|[0048] Strain Qian2 was inoculated onto YMA solid medium for activation, purified by transfer on solid plates 3-4 times, and the purified strain was inoculated into YMA liquid medium at an inoculum size of 1.5% and cultured at 28 ℃ for 5 days to obtain a slow rhizobium Qian2 inoculum.|[0049] Mixing the prepared bacillus brevis v6 microbial inoculum, the nitrifying bacillus XY-01 microbial inoculum, the free-living nitrogen fixing bacterium MBC5 microbial inoculum and the slow rooting tumor fungus Qian2 microbial inoculum according to the volume ratio of 1:1:2:3 to obtain a composite microbial inoculum, and uniformly mixing biochar, straw fragments and the composite microbial inoculum according to the dosage ratio of 5g to 3g to 10mL to obtain the soil carbon fixing agent.|[0050] 3. Loess plateau abandoned land soil carbon fixation capacity improvement test|[0051] 1. Overview of test zone|[0052] The test area is located in the Wuli gulf region (36 DEG 51 '-36 DEG 53' N,109 DEG 20 '-109 DEG 22' E) of Ansai area of Yanan city of Shaanxi province, and the altitude is 1010-1400 m, and belongs to a typical loess hilly and gully area. The area belongs to a moderate temperate zone continental semiarid monsoon climate, the average air temperature is 8.8 ℃ for many years, the average annual evapotranspiration is 1490mm, the average annual rainfall is 505mm, most rainfall is concentrated in 7-9 months, and the rainfall accounts for about 70% of the annual rainfall. The annual average frost free period is about 157d. The soil in the flow area is mainly yellow cotton soil developed from aeolian loess matrix, has loose soil texture, poor erosion resistance and serious water and soil loss. Currently, 184.18hm 2 is a major type of land use in the penta-gulf stream. The method mainly comprises the steps of rotation planting of corns (Zea mays) and millet (SETARIA ITALICA) before the farmland is abandoned, double cropping in one year, extensive farmland management, no fertilization, irrigation mainly depends on rainfall, all overground parts are removed after crops are harvested, 2 times of intertillage are carried out in a growing season, and the depth is 20cm. No artificial interference exists during the period of barren, and vegetation naturally colonizes and grows.|[0053] 2. Test design|[0054] The present invention selects 1 farmland which was abandoned in 1999 as a test land in the five-gulf stream region in 2001, and the area is about 20m x 20m. 12 cells were randomly established within the experimental plot, each cell having an area of 4m by 5m and a spacing of about 5m from each other. The cell adopts a random block design, wherein the group A is carbon fixing agent adding treatment, the group B is plant community structure adjusting treatment, the group AB is interaction treatment between the group A and the group B, the group CK is a control group, no treatment is carried out, and each treatment is repeated for 3 times. The group A cells (A1, A2 and A3) apply the carbon strengthening agent according to the standard of 10 kg/mu each year without other treatment, the group B cells (B1, B2 and B3) adjust the plant community composition every 5 years without other treatment, and the group AB cells (AB 1, AB2 and AB 3) apply the carbon strengthening agent according to the standard of 10 kg/mu each year and adjust the plant community composition every 5 years. All experiments were started in 2002, vegetation surveys were conducted every 5 years for all cells, and soil samples were collected to analyze the change in carbon sequestration capacity of the abandoned land soil.|[0055] 3. Vegetation investigation method|[0056] And carrying out vegetation investigation in a season of 7 months when vegetation grows vigorously. 51 m hand pieces were laid out in total at the four corners and center of each cell for vegetation investigation. The seed names of all plants, the number of all plant species, the total number of plants per plant, and the coverage of each plant within each panel were recorded. The coverage was assessed visually. All investigation was done jointly by both investigators to reduce human error and finally all investigation data were collated for subsequent analysis.|[0057] 4. Soil sample collection and carbon fixation capacity measurement|[0058] 10 Sampling points are selected in each cell according to an S-shaped sampling method, and after surface fallen matters and humus layers are removed, soil drills with the inner diameter of 5cm are used for collecting surface soil samples with the inner diameter of 0-10 cm. 10 samples in the same district are evenly mixed, sieved by a sieve of 2mm, put into a self-sealing bag and placed into a portable refrigerator for transportation back to a laboratory. The soil sample is divided into two parts, one part is naturally air-dried, and the other part is stored at 4 ℃ and used for the subsequent analysis of the carbon fixing capacity of the soil. In addition, 3 soil sections are randomly selected in each district, and a ring cutter with the volume of 100cm 3 is used for collecting surface layer undisturbed soil samples with the volume of 0-10cm for measuring the soil volume weight.|[0059] Soil organic carbon reserves (Soil organic carbon stock, SOCs) and soil active organic carbon components and refractory organic carbon components are selected to represent the carbon fixing capacity of the soil. Wherein the soil-active organic carbon component comprises microbial biomass carbon (Microbial biomass carbon, MBC), readily oxidizable organic carbon (PERMANGANATE OXIDATIVE ORGANIC CARBON, POXC) and particulate organic carbon (Particulate organic carbon, POC), representing the physical, chemical and biological components of the soil-active organic carbon, respectively, and further wherein the refractory organic carbon component is represented by soil-inert organic carbon (RECALCITRANT ORGANIC CARBON, ROC). The measurement and calculation methods of the above-mentioned index are as follows.|[0060] The organic carbon (Soil organic carbon, SOC) content of the soil is measured by adopting a potassium dichromate-concentrated sulfuric acid external heating capacity method. The soil volume weight is measured by adopting a drying method, namely, a soil sample in the cutting ring is dried to constant weight at 105 ℃, and the dried soil weight per unit cutting ring volume is calculated by weighing to obtain the soil volume weight. Soil organic carbon reserves are calculated according to the following formula:|[0061] SOCS=SOC x D x BD x K|[0062] Wherein SOCs is soil organic carbon reserve (kg/m 2), SOC is soil organic carbon content (g/kg), D is soil thickness (cm), BD is soil volume weight (g/cm 3), and K is a constant of 0.01. |[0063] The carbon (MBC) content of the soil microorganisms is measured by a chloroform fumigation extraction method. 20g of soil samples stored in duplicate at 4℃were weighed into petri dishes, one for chloroform fumigation and the other for no fumigation. The fumigated soil was placed in a desiccator with 5 beakers at the bottom, two of which were each charged with 30mL of chloroform, the other two beakers were charged with 30mL of distilled water, and the last beaker was charged with 30mL of 0.5mol/L sodium hydroxide solution to absorb CO 2 released from the soil. The non-fumigated soil sample was placed in a desiccator with 3 beakers at the bottom, wherein 30mL of distilled water was added to each of the two beakers, and the other 30mL of 0.5mol/L sodium hydroxide solution was added. The desiccator was evacuated and placed in a 25℃incubator for dark culture for 24h. After the cultivation, 12.5g of fumigated and unfused soil samples were weighed and placed in 100mL Erlenmeyer flasks, respectively, 50mL of 0.5mol/L potassium sulfate solution was added, followed by shaking on a 25℃shaker for 30min (200 rpm/min). After filtration, the carbon content in the solution is measured by using an Shimadzu TOC instrument, and the MBC content is the difference value of the carbon content of fumigated and unfused soil samples.|[0064] The content of the easily-oxidizable organic carbon (POXC) in the soil is measured by adopting a potassium permanganate oxidation colorimetric method. 6-10g of air-dried soil samples (ensuring that the carbon content of each sample is in the range of 15-30 mg) were weighed into 50mL centrifuge tubes and used as a blank (no soil sample added). 25mL of 333mmol/L potassium permanganate solution was added, mixed well and placed on a 25℃shaker and shaken for 1h (250 rpm/min). After completion, the tube was centrifuged in a centrifuge at 4800rpm/min for 5 minutes, and the supernatant was diluted 1000/3 times with ultrapure water, and the absorbance of the diluted solution was measured at 565nm with a spectrophotometer. 1mmol/L of potassium permanganate consumes 9mg of carbon in the oxidation process, and the amount of consumed potassium permanganate is calculated according to the difference between the absorbance values of the blank control and the sample solution, so that the POXC content is calculated.|[0065] The organic carbon (POC) content of the soil particles is measured by adopting a sodium hexametaphosphate extraction method. Weighing 20g of air-dried soil sample, placing the air-dried soil sample in a 250mL conical flask, adding 60mL of 5g/L sodium hexametaphosphate solution, shaking the flask by hands for 10-15min, placing the flask on a shaking table for dispersing for 18h (18 ℃ and 90 rpm/min), sieving the dispersion liquid with a 53 mu m sieve, washing the solution with ultra-pure water until the water below the sieve is clear, placing the upper part of the sieve into a granular organic matter, drying the granular organic matter at 80 ℃ for 24h, weighing and calculating the percentage of the granular organic matter in the soil. Grinding the dried granular organic matters, sieving with a 0.149mm sieve, taking a certain weight of the granular organic matters, measuring the carbon content of the granular organic matters by using a potassium dichromate-concentrated sulfuric acid external heating capacity method, multiplying the carbon content by the percentage of the soil, and calculating the POC content.|[0066] The inert organic carbon (ROC) content of the soil is determined by a hydrochloric acid digestion method. 2g of the air-dried soil sample passing through a 1mm sieve is weighed and placed in a 100mL digestion tube, 5mL of 6mol/L hydrochloric acid solution is added and digested for 16h at 125 ℃. The digested soil sample was transferred to a 50mL centrifuge tube, 30mL distilled water was added, shaken vigorously, and centrifuged for 3min in a 4000rpm/min centrifuge. The supernatant was removed, 30mL of distilled water was again added, and the above procedure was repeated 5 times until the hydrochloric acid was thoroughly washed. The cleaned soil sample was dried at 55 ℃ and then assayed for ROC content using potassium dichromate-concentrated sulfuric acid external heating capacity.|[0067] 5. Plant community composition of control group (CK) and soil carbon fixation capacity change|[0068] According to the above-mentioned vegetation investigation method and soil index measurement method, the plant community group (tables 1 and 2) and the soil carbon fixation ability change (shown in Table 3) of the control abandoned land were examined in 2002-2022.|[0069] Table 1 changes in plant population composition in control plots 2002-2007|[0070] |[0071] |[0072] |[0073] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0074] Table 2 2012-2022 changes in plant population composition in control plots|[0075] |[0076] |[0077] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0078] Table 3 changes in soil carbon sequestration Capacity in the control group of 2002-2022 abandoned lands|[0079] |[0080] Note that the data are mean ± standard error, and that the same column of different lower case letters indicates significant differences between different years (P < 0.05).|[0081] The results shown in tables 1 and 2 demonstrate that in 2002-2022, 56 plants were counted in the control group cells and were belonging to 22 families, 6 of gramineae, 4 of leguminous plants and 18 of Compositae. On average, the densities of Gramineae, leguminosae and Compositae were 11.80 strain/m 2, 0.83 strain/m 2 and 21.38 strain/m 2, respectively, and the coverage was 17.65%, 1.94% and 35.01%, respectively. The density and coverage of gramineae and leguminous plants tended to increase during the test period, but the gramineae was not significantly increased, and the overall density and coverage were not high despite the tremendous increase in leguminous plants.|[0082] The contribution of three grasses, such as mesona, oak and Cryptocarya, to the density and coverage of the community of the plant in the barren land increases year by year, increasing from 0.48% and 1.11% in 2002 (density contribution) to 23.60% and 31.14% in 2022, respectively, and likewise, the contribution of three leguminous plants, such as Pisum album, astragalus trifoliatus and Lespedeza multiflora, to the density and coverage of the community of the plant in the barren land increases year by year, increasing from 0% and 0% in 2002 to 2.89% and 5.47% in 2022, respectively. In addition, the contributions of the three kinds of plants of the asteraceae family, namely the spanishneedles herb, the herba artemisiae capillaris and the herba artemisiae annuae to the community density and the coverage of the abandoned barren land are 22.02-29.32% and 29.16-47.66% respectively, but no obvious annual change trend exists.|[0083] As is clear from Table 3, in 2002-2022, the organic carbon reserves, the microbial carbon, the readily oxidizable organic carbon and the particulate organic carbon contents of the soil increased year by year (P < 0.05), the average increases were 29.55%, 75.90%, 253.33% and 57.82%, respectively, but the inert organic carbon contents of the soil did not change significantly, the average increases during the test were 13.80%, and the above results generally indicate that the soil carbon fixing ability of the control group increased slowly.|[0084] 6. Soil carbon fixation capacity improvement test of abandoned land|[0085] Starting in 2002, carbon fixing agents are spread on the soil surfaces of AB1, AB2 and AB3 cells according to the application amount of 10 kg/mu every year, and plant community structures are adjusted once in 2002, 2007, 2012, 2017 and 2022 respectively.|[0086] The specific implementation process of the plant community structure adjustment is as follows:|[0087] (1) Leguminous and gramineous plant reseeding |[0088] In the test, lespedeza multiflora, astragalus trifolitan, viola yessoensis, cynanchum komarovii and Gramineae are selected and planted in a mixed mode. The sowing quantity of each grass seed in the mixed sowing combination is calculated by the product of the mixed sowing proportion of the grass seed in the mixed sowing combination and the single sowing quantity of the grass seed. Wherein, the unicast amount of the Lespedeza multiflora, the trifolith astragalus root, the field pea, the goose grass, the Phryegrass and the elymus is 5.0 kg/mu, 2.5 kg/mu, 1.5 kg/mu and 2.0 kg/mu respectively. The ratio of bean-grass mixed sowing (mixed sowing of leguminous plants and gramineous plants) is 1:1, and the total sowing amount is 2.5 kg/mu. Thus, the sowing amount of the Lespedeza multiflora, the trifolith astragalus membranaceus, the vetch, the mesona chinensis, the crypt-seed grass and the elymus-cape grass is respectively 0.835 kg/mu, 0.415 kg/mu, 0.25 kg/mu and 0.335 kg/mu when the beans-grass are mixed.|[0089] The 6 grass seeds are fully and uniformly mixed and then soaked in warm water at 45 ℃ for 24 hours, and after soaking, the grass seeds are sown in the same row, each cell is sown in the same row in a supplementary mode, the row spacing is 30cm, and the sowing depth is 2cm. The method comprises the steps of first-time supplementary seeding in 2002, 2007, 2012, 2017 and 2022 respectively, not applying fertilizer, not irrigating and not mowing after seeding, carrying out vegetation investigation in the vegetation growth vigorous period at the end of 7 months in the current year, and collecting soil samples to analyze the carbon fixation capacity of the soil.|[0090] The mesona blume seeds and the cryptopsis subulata seeds are purchased from Jiangsu Xin Rui seed industry Co., ltd, the Alternaria alternata seeds, the Vicia and the Lespedeza multiflora seed seeds are purchased from Jiangsu Gangren Bozier seed industry Co., ltd, and the Daghestan astragalus seed is provided by the grassland research of the national academy of agricultural and animal husbandry of inner Mongolian. The germination rate of all grass seeds is 73% -89%, the water content is 3% -12%, the purity is 80% -90%, and the variety purity is 90% -95%.|[0091] (2) Compositae dominant species removal|[0092] To ensure the removal effect, the removal of the dominant species of the asteraceae plants was completed in the previous year of the leguminous and gramineous plants' complementary sowing, i.e. the whole root of the spanishneedles herb, the artemisia capillaris and the artemisia capillaris in the test cell was removed at the end of 7 months of 2001, 2006, 2011, 2016 and 2021, respectively.|[0093] Meanwhile, in the test communities A1, A2 and A3,2002-2022, the carbon fixing agent is sprayed every year according to the application amount of 10 kg/mu, the plant community composition is not changed artificially, vegetation surveys are respectively carried out at the end of 7 months of 2002, 2007, 2012, 2017 and 2022, and soil samples are collected to analyze the carbon fixing capacity of the soil.|[0094] In addition, for test cells B1, B2 and B3, plant colony structures were adjusted at the beginning of 4 months in 2002, 2007, 2012, 2017 and 2022, respectively, the specific operation was as described above, but no carbon strengthening agent was applied, and vegetation surveys were conducted at the end of 7 months in 2002, 2007, 2012, 2017 and 2022, respectively, and soil samples were collected to analyze soil carbon fixation ability.|[0095] 4. Analysis of experimental results|[0096] 1. Influence of carbon sequestration agent on carbon sequestration capacity of soil in loess plateau|[0097] After applying only the carbon fixing agent, the plant community composition (table 4 and table 5) and the carbon fixing ability change of the soil (as shown in table 6) on the land of the barren lands in 2002, 2007, 2012, 2017 and 2022.|[0098] Table 4 changes in plant community composition in the abandoned lands where the carbon reinforcing agent was applied alone in 2002-2007|[0099] |[0100] |[0101] |[0102] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0103] Table 5 2012-2022 Change in plant community composition of abandoned land with carbon reinforcing agent applied alone|[0104] |[0105] |[0106] |[0107] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0108] As can be seen from tables 4 and 5, in 2002-2022, 62 plants were counted in the cell to which only the carbon strengthening agent was applied, and the plants were classified into 24 families, wherein 6 plants of Gramineae, 5 plants of Leguminosae, and 20 plants of Compositae were counted. On average, the densities of Gramineae, leguminosae and Compositae were 12.23 strain/m 2, 1.26 strain/m 2 and 22.23 strain/m 2, respectively, and the coverage was 20.17%, 2.20% and 33.08%, respectively. Similar to the control group, the density and coverage of both Gramineae and Leguminosae plants tended to increase during the test, but the enhancement of Gramineae was not obvious, and the overall density and coverage were not high despite the tremendous enhancement of Leguminosae plants. In general, the application of the carbon fixing agent increases the species richness of the community of plants in the abandoned land, increases the density of the grasses, legumes and asteraceae plants, increases the coverage of the grasses and legumes, but decreases the coverage of the asteraceae plants.|[0109] Specifically, after the application of the carbon fixing agent, the contribution of three grasses of the order Centipeda minima, oak and Cryptotaea has been increased year by year from 3.61% (density contribution) and 4.28% (coverage contribution, the same applies hereinafter) in 2002 to 23.84% and 31.87% in 2022, respectively, and the contribution of three leguminous plants of the order Daphne, astragalus trifoliatus and Lespedeza multiflora to the plant community density and coverage has also been increased year by year from 1.22% and 1.35% in 2002 to 4.39% and 4.24% in 2022, respectively. In addition, the contributions of the three kinds of plants of the asteraceae family, namely the spanishneedles herb, the herba artemisiae capillaris and the herba artemisiae annuae to the community density and the coverage of the abandoned barren land are respectively 15.01-36.33% and 17.56-34.28%, and the obvious annual change trend does not exist.|[0110] Compared with the control group, the application of the carbon strengthening agent improves the density of gramineae, leguminous and Compositae plants by 3.73 percent, 74.42 percent and 4.37 percent on average, and improves the density of the three gramineae plants, the three leguminous plants and the three Compositae plants by 212.86 percent, 91.64 percent and 5.11 percent on average compared with the control group. In addition, the application of the carbon fixing agent increases the coverage of gramineae and leguminous plants by 17.31% and 104.31% respectively compared with the control group, but reduces the coverage of Compositae plants by 4.95% compared with the control group, and likewise, the application of the carbon fixing agent increases the coverage of the three gramineae plants and the three leguminous plants by 192.03% and 221.01% respectively compared with the control group, but reduces the coverage of the three Compositae plants by 19.30% compared with the control group.|[0111] Table 6 changes in carbon sequestration Capacity of the abandoned land soil with only carbon sequestrants applied in 2002-2022|[0112] |[0113] Note that the data are mean ± standard error, and that the same column of different lower case letters indicates significant differences between different years (P < 0.05).|[0114] The results shown in Table 6 demonstrate that in 2002-2022, the soil organic carbon reserves, microbial carbon, readily oxidizable organic carbon and particulate organic carbon content of the carbon-reinforcing agent cells were only increased year by year (P < 0.05), with average increases of 58.33%, 105.24%, 177.27% and 30.32%, respectively, and the soil inert organic carbon content was not significantly changed, with average increases of 21.64% during the test. In addition, the application of the carbon fixing agent increases the carbon fixing capability index of the 5 soil by 86.74%, 25.31%, 28.57%, 21.30% and 13.12% respectively compared with the control group, which indicates that the carbon fixing capability of the abandoned land soil can be improved to a certain extent by only applying the carbon fixing agent.|[0115] 2. Regulating influence of plant community structure on carbon fixation capacity of loess plateau abandoned land soil|[0116] Changes in carbon sequestration capacity of soil after adjustment of plant community species composition alone on the lands of the barren lands 2002, 2007, 2012, 2017 and 2022 are shown in tables 7 and 8, respectively.|[0117] Table 7 2002-2007 changes in plant community composition of the abandoned land for which plant community structure was adjusted only|[0118] |[0119] |[0120] |[0121] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0122] Table 8 2012-2022 changes in plant community composition of the abandoned land for plant community structure adjustment only|[0123] |[0124] |[0125] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0126] As is clear from tables 7 and 8, in 2002-2022, the total statistics of 55 plants in the cell with the plant community structure were adjusted to be 21 plants, wherein 9 plants of Gramineae, 6 plants of Leguminosae and 15 plants of Compositae were used. On average, the densities of Gramineae, leguminosae and Compositae were 16.47 strain/m 2, 9.69 strain/m 2 and 14.65 strain/m 2, respectively, and the coverage was 35.84%, 20.83% and 17.69%, respectively. The density and coverage of each of the Gramineae, leguminosae and Compositae plants are not greatly changed with time due to the regular adjustment of the plant community composition, but compared with the control group, the adjustment of the plant community structure obviously improves the species uniformity of the plant community in the abandoned lands, increases the density and coverage of the Gramineae and Leguminosae plants, and reduces the density and coverage of the Compositae plants.|[0127] Specifically, after plant community structure is adjusted, the contribution of three grasses of herba chenopodii, herba Oenotherae Erythrosepalae and Cryptotaenia japonica to the community density and coverage of the abandoned barren land is 26.90% -28.90% and 35.17% -42.58%, the contribution of three leguminous plants of herba Violae, radix astragali Melilotoidis and Lespedeza multiflora to the community density and coverage of the abandoned barren land is 16.03% -18.50% and 20.94% -28.02%, and the contribution of three kinds of plants of the Compositae of herba Bidentis Bipinnatae, herba Artemisiae Scopariae and herba Artemisiae Scopariae to the community density and coverage of the abandoned barren land is 4.58% -12.06% and 2.89% -11.35%, respectively, and no obvious annual change trend is shown.|[0128] Compared with the control group, the density of the gramineae and leguminous plants is improved by 40.43 percent and 1665.89 percent respectively by adjusting the plant community structure, and the density of the three gramineae plants and the three leguminous plants is improved more than that of the control group, and the increase of the gramineae plants and the leguminous plants is 1778.85 percent and 1897.08 percent respectively. In addition, the plant community structure is adjusted to increase the coverage of gramineae and leguminous plants by 125.95% and 2358.63% respectively compared with the average coverage of the control group, and the coverage of the three gramineae plants and leguminous plants is increased by 1920.01% and 5010.22% respectively compared with the average coverage of the control group. In contrast, after plant colony structure was adjusted, the densities and coverage of the asteroid plants were reduced by 30.38% and 48.89% respectively compared to the control group, and in particular, the densities and coverage of the three asteroid plants were reduced by 64.47% and 76.55% respectively compared to the control group.|[0129] Table 9 2002-2022 changes in carbon sequestration ability of the soil of abandoned lands in which plant colony structures were regulated alone|[0130] |[0131] Note that the data are mean ± standard error, and that the same column of different lower case letters indicates significant differences between different years (P < 0.05).|[0132] As can be seen from Table 9, after the plant community structure was adjusted, the average increases in soil organic carbon reserves, microbial biomass carbon, readily oxidizable organic carbon, particulate organic carbon and inert organic carbon content were 20.69%, 115.31%, 211.11%, 108.97% and 9.52%, respectively, over the year 2002-2022, and although the various indices characterizing the soil carbon fixing ability generally tended to increase over time, the differences in soil organic carbon reserves and inert organic carbon content did not reach significant levels over the different years. In addition, the plant community structure is adjusted to ensure that the organic carbon reserves, the microbial biomass carbon, the easily oxidized organic carbon and the inert organic carbon content of the soil are respectively increased by 25.89%, 6.88%, 14.00% and 2.16% compared with the control group, but the organic carbon content of soil particles is reduced by 28.44% compared with the control group, and the result shows that the carbon fixing capability of the soil in the barren lands can be improved to a certain extent by only adjusting the plant community structure, but the effect is lower than that of the treatment by only applying the carbon fixing agent.|[0133] 3. The invention has the effect on the carbon fixation capacity of the soil of the loess plateau abandoned barren land|[0134] The changes in the carbon sequestration ability of the soil after applying the carbon sequestration agent and adjusting the plant community structure on the land of the barren lands 2002, 2007, 2012, 2017 and 2022 are shown in tables 10 and 11, respectively.|[0135] Table 10 2002-2007 changes in the composition of the plant communities of the abandoned land in which the present invention was practiced|[0136] |[0137] |[0138] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0139] Table 11 2012-2022 Change in plant community composition in the abandoned land where the invention was practiced|[0140] |[0141] |[0142] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0143] As is clear from tables 10 and 11, in 2002-2022, 59 plants were counted in the cell in which the present invention was practiced, and the plants were belonging to 23 families, wherein 10 plants of Gramineae, 9 plants of Leguminosae, and 15 plants of Compositae. On average, the densities of the gramineae, leguminous and asteraceae plants were 17.10 strain/m 2, 9.78 strain/m 2 and 13.47 strain/m 2, respectively, with coverage levels of 35.40%, 20.66% and 19.16%, respectively. After the invention is implemented, the density and coverage of the gramineae, leguminous and asteraceae plants are not greatly different from those of the cells with the structure of the plant community, but compared with the control group and the application of the carbon strengthening agent, the invention obviously improves the species uniformity of the plant community of the barren lands, increases the density and coverage of the gramineae and leguminous plants, and reduces the density and coverage of the asteraceae plants.|[0144] Specifically, after the invention is implemented, the contributions of three gramineous plants of herba chenopodii, herba Oenotherae Erythrosepalae and cryptotaenia japonica to the community density and coverage of the abandoned lands are 24.29% -34.16% and 32.97% -41.85%, the contributions of three leguminous plants of herba Violae, radix astragali and Lespedeza multiflora to the community density and coverage of the abandoned lands are 16.00% -18.94% and 14.93% -25.91%, and the contributions of three kinds of plants of the jektight, herba Artemisiae Scopariae and herba Artemisiae Scopariae to the community density and coverage of the abandoned lands are 3.13% -10.93% and 2.22% -6.22%, respectively, and the obvious annual change trend is not shown.|[0145] Compared with the control group, the density of the gramineae and the leguminous plants is averagely improved by 45.70 percent and 1672.06 percent, the density of the gramineae and the leguminous plants is improved by more than 1895.93 percent and 2000.47 percent compared with the control group, and the coverage of the gramineae and the leguminous plants is averagely improved by 122.72 percent and 2465.90 percent compared with the control group, and the coverage of the gramineae and the leguminous plants is improved by 1859.14 percent and 6167.90 percent compared with the control group. In contrast, the densities and coverage of the asteraceae plants were reduced by 36.04% and 44.87% on average, respectively, compared to the control group, and the densities and coverage of the three asteraceae plants were reduced by 70.46% and 86.07% on average, respectively.|[0146] Table 12 2002-2022 Change in the carbon sequestration Capacity of the soil in the abandoned land where the invention was practiced|[0147] |[0148] |[0149] Note that the data are mean ± standard error, and that the same column of different lower case letters indicates significant differences between different years (P < 0.05).|[0150] As can be seen from table 12, the carbon fixing agent was applied while adjusting the plant community structure to significantly improve the soil carbon fixing ability of the abandoned lands, and the average increases in the soil organic carbon reserves, microbial carbon, readily oxidizable organic carbon, particulate organic carbon and inert organic carbon content between 2002-2022 were 66.67%, 148.00%, 169.23%, 77.48% and 34.81%, respectively (P < 0.05). Compared with a control group, the method ensures that the indexes for representing the soil carbon fixing capacity of the 5 indexes are respectively increased by 153.38%, 47.45%, 51.93%, 17.39% and 17.85% compared with the average indexes of the control group, and the results of different treatments show that the method has the best effect of improving the soil carbon fixing capacity.|[0151] 4. Effect contrast of improving carbon fixation capacity of soil of abandoned wasteland by different treatments|[0152] Table 13 2002-2022 comparison of soil carbon sequestration improvement effects for different treatments compared to control group|[0153] |[0154] |[0155] Note that the data are mean ± standard error.|[0156] Table 13 shows the increase in carbon sequestration capacity of the barren land soil over the control group in 2002, 2007, 2012, 2017 and 2022 after applying only the carbon sequestration agent, adjusting only the plant community structure and practicing the invention. It can be seen that:|[0157] (1) In addition, the invention can improve the carbon fixation capacity of soil by only applying the carbon strengthening agent and only adjusting the plant community structure, but the effect is obviously lower than that of the invention, and particularly, the invention can improve the organic carbon reserves, the microbial carbon content, the easily-oxidizable organic carbon content and the inert organic carbon content of soil by 1.77 times, 1.80 times, 1.79 times and 1.35 times of the effect of only applying the carbon strengthening agent respectively on average and 5.84 times, 5.39 times, 2.75 times and 6.02 times of the effect of only adjusting the plant community structure respectively. |[0158] (2) In 2002-2022, the invention can respectively and averagely increase the organic carbon reserves, the microbial carbon content, the easily-oxidized organic carbon content, the granular organic carbon content and the inert organic carbon content by 152.84 percent, 49.98 percent, 67.96 percent, 18.00 percent and 19.45 percent, particularly, the indexes 5 can respectively increase 126.67 percent, 13.70 percent, 82.91 percent, 3.10 percent and 10.57 percent in the current year of the invention, and the lifting effect is in an overall year-by-year increasing trend, which indicates that the invention can rapidly, effectively and continuously improve the carbon fixing capability of the soil of the loess plateau and the barren land, and can be popularized and applied.|[0159] While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the following claims be interpreted as including the preferred embodiments and all such alterations and modifications as fall within the scope of the invention.|[0160] It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof. (CN116420457)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of carbon fixation, in particular to a method for improving the carbon fixation capacity of soil of a loess plateau abandoned land.|BACKGROUND ART|[0002] The loess plateau ecological environment fragile zone and the climate change sensitive area are one of main battlefields for ecological protection and high-quality development of yellow river basin. The coverage of loess plateau vegetation is improved from 31.6% in 1999 to 62.8% in 2018, soil erosion is effectively controlled, ecological environment quality is obviously improved, and regional carbon sink function is obviously improved. The area of the loess plateau farmland is 5.7 multiplied by 10 6hm2, which accounts for 10.4 percent of the total area of grasslands in the area, the organic carbon sequestration potential of the soil on the surface layer of the loess plateau can reach 8.3t/hm 2, and the method plays an important role in the loess plateau and even the carbon budget of China. However, the carbon fixation rate of the soil of the abandoned land is slow, and the effective exertion of the carbon sink function of the ecological system is severely restricted. The reason for this is the dependence of soil carbon sequestration on functional microorganisms and plant functional groups. For example, biochar Shi Junfei can raise the carbon storage of the abandoned land soil by 10.62% within 30 days. In addition, the dominant plant functional group species in the later period of the back-up succession of the primary period of the back-up period can increase the carbon fixation rate of the soil by 200%. In view of the importance of the abandoned land in maintaining the functions of loess plateau carbon sink, the improvement of the soil carbon fixation capacity of the abandoned land is of great significance in reducing the regional atmospheric carbon dioxide concentration, reducing the greenhouse effect and the negative ecological influence thereof.|[0003] An Ansai area belongs to Yanan city of Shanxi province, and is in loess plateau abdomen area, fragile in ecological environment, serious in water and soil loss and extremely low in carbon content in soil. At present, ecological restoration of Ansai areas is mainly carried out on low-yield farmlands, namely, degraded lands are restored by natural succession of vegetation after the lands. However, long-term abandoned lands have slow effects in restoring soil structures, improving soil nutrient levels, improving soil microbial systems and the like, and the succession of plant communities on the land has extremely large uncertainty, so that the soil carbon fixation effect of the abandoned lands is not obvious, and even the carbon reserves of the abandoned lands after 30 years of abandoned lands have a trend of reduction. Therefore, the improvement of the carbon sequestration and sink enhancement capability of the abandoned land soil through manual intervention is particularly important.|DISCLOSURE|Disclosure of Invention|[0004] In order to solve the technical problems, the invention provides a method for improving the carbon fixing capability of loess plateau abandoned land soil, which is characterized in that a carbon fixing agent is applied to the soil, and the plant community structure is adjusted to improve the carbon fixing capability of the soil.|[0005] The invention provides a method for improving the carbon fixation capacity of loess plateau abandoned land soil, which comprises the steps of applying a carbon strengthening agent into the soil and adjusting plant community structures;|[0006] The carbon fixing agent is prepared from biochar, straw fragments and a composite microbial agent according to the dosage ratio of 4-6g to 2-3g to 6-10 mL; |[0007] The composite microbial inoculum is prepared by mixing a bacillus brevis v6 microbial inoculum, a nitrifying bacillus XY-01 microbial inoculum, an authigene nitrogen fixing bacterium MBC5 microbial inoculum and a slow rooting tumor bacterium Qian2 microbial inoculum according to the volume ratio of 1:1:2-3:2-4; |[0008] the plant community structure adjustment specifically comprises the step of supplementing leguminous plants and gramineous plants, and the number of dominant species of the asteraceae plants is reduced. |[0009] Further, the preparation process of the bacillus brevis v6 microbial inoculum comprises the steps of inoculating a strain v6 to an LB solid culture medium for activation, carrying out purification through 3-4 times of flat streak transfer, inoculating the purified strain into an LB liquid culture medium according to the inoculum size of 1.5%, and culturing for 4 days at 28 ℃ to obtain the bacillus brevis v6 microbial inoculum.|[0010] Further, the preparation process of the Nitrobacter vickers XY-01 microbial inoculum comprises the steps of inoculating a bacterial strain XY-01 to an HA solid culture medium for activation, carrying out purification through 3-4 times of plate streak transfer, inoculating the purified bacterial strain into the HA liquid culture medium according to the inoculum size of 1.5%, and culturing for 3 days at the temperature of 28 ℃ to obtain the Nitrobacter vickers XY-01 microbial inoculum.|[0011] The preparation process of the free-living nitrogen fixing bacteria MBC5 microbial inoculum comprises the steps of inoculating bacterial strain MBC5 to a GD solid culture medium for activation, transferring the bacterial strain onto a solid flat plate for 3-4 times for purification, inoculating the purified bacterial strain into a GD liquid culture medium according to the inoculation amount of 1.5%, and culturing for 3 days at 28 ℃ to obtain the free-living nitrogen fixing bacteria MBC5 microbial inoculum.|[0012] Further, the preparation process of the slow rhizobia Qian2 microbial inoculum comprises the steps of inoculating the strain Qian2 onto YMA solid medium for activation, carrying out purification by transferring on a solid plate for 3-4 times, inoculating the purified strain into YMA liquid medium according to the inoculum size of 1.5%, and culturing at 28 ℃ for 5 days to obtain the slow rhizobia Qian2 microbial inoculum.|[0013] Further, the application amount of the carbon fixing agent is 5-10 kg/mu.|[0014] The plant community structure adjustment specifically comprises the step of supplementing and sowing the leguminous plants and the gramineous plants in the soil, so that the number of dominant species of the asteraceae plants is reduced.|[0015] Further, the leguminous plants include Lespedeza multiflora, astragalus trifolitan and Viola yedoensis.|[0016] Further, the gramineous plants include mesona blume, cryptotaenia japonica and conyza sativa.|[0017] Further, the dominant species of the Compositae plant mainly comprise Bidens parviflora, artemisia annua and Artemisia capillaris.|[0018] Further, the leguminous plants and the gramineous plants are mixed-sown;|[0019] the seeding amount of the Lespedeza multiflora, the trifolith astragalus root, the field peas, the herba mesonae chinensis, the cryptotaenia japonica and the elymus cape is respectively 0.835 kg/mu, 0.415 kg/mu, 0.25 kg/mu and 0.335 kg/mu. |[0020] Compared with the prior art, the invention has the beneficial effects that:|[0021] 1. According to the invention, the carbon fixing agent formed by compounding the biochar, the straw fragments and the composite microbial inoculum is applied to the soil, on one hand, the soil carbon fixing is increased while the soil nitrogen fixing effect and the nitrification effect are promoted through reconstruction of the microbial nitrogen fixing flora, and the growth environment of plant root systems can be improved and the root system development is accelerated through improvement of the microbial flora of the soil, so that the aim of increasing the underground soil carbon accumulation is achieved. On the other hand, porous biochar can adsorb a large amount of carbon components, improve the carbon reservoir capacity of soil and increase the carbon reservoir stability. |[0022] 2. The invention relates to a method for preparing a plant with high photosynthetic carbon fixation efficiency, which comprises the steps of taking a asteraceae plant as a pioneer species of loess plateau, evolving unique physiological morphological characteristics in the process of adapting to drought and barren, such as scale-shaped, strip-shaped, columnar or needle-shaped blades which are beneficial to water conservation, but also causing the photosynthesis carbon fixation efficiency of the unit leaf area of the asteraceae plant to be low, capturing a large amount of photothermal soil resources by a large plant and developed root system of the asteraceae plant, and influencing the photosynthesis carbon fixation of other short plants;|[0023] 3. The invention can increase the overground vegetation coverage, plant diversity and species richness by reducing the number of dominant species of the asteraceae plants, reduce the carbon loss risk caused by soil erosion and play a role in soil conservation, water conservation, fertilizer conservation and carbon fixation; |[0024] 4. the feeding value of the asteraceae plants is generally lower than that of grasses of graminees and leguminous plants, and the native leguminous plants and the grasses of the invention have strong adaptability and high survival rate, can increase the yield of pastures with better palatability, and improve the economic benefit of abandoned lands; |[0025] 5. The method provided by the invention can realize the linkage effect of 'plant photosynthetic carbon fixation-microorganism carbon promotion by nitrogen-biochar carbon adsorption' by applying the carbon strengthening agent and adjusting the plant community structure, increases the combined carbon fixation effect of the soil on the land and the underground of the loess plateau, cooperatively improves the carbon fixation capacity, the carbon warehouse reserves and the carbon warehouse stability of the soil, is natural and environment-friendly, has strong operability, is easy to realize and popularize, can rapidly, effectively and continuously improve the carbon fixation capacity of the soil, and can be suitable for the land of the loess plateau and other types of grasslands. |INVENTION MODE|Detailed Description|[0026] The following detailed description of specific embodiments of the invention is, but it should be understood that the invention is not limited to specific embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. The experimental methods described in the examples of the present invention are conventional methods unless otherwise specified, and materials, reagents, etc. used in the examples described below are commercially available.|[0027] Example 1|[0028] The embodiment provides a method for improving the carbon fixation capacity of soil of a loess plateau abandoned land.|[0029] 1. Experimental materials|[0030] 1. Material source|[0031] The biochar used in the invention is commercially available biochar;|[0032] The straw scraps used in the invention are obtained by crushing commercial straw; |[0033] The nitrifying short bacillus v6 is purchased from the China general microbiological culture collection center with the preservation number GDMCC NO:60296, the nitrifying bacillus XY-01 is purchased from the China general microbiological culture collection center with the preservation number CGMCC No.10171, the authigenic nitrogen fixing bacterium MBC5 is purchased from the China general microbiological culture collection center with the preservation number CGMCC No.10821, and the slow-growing rhizobium Qian2 is purchased from the China general microbiological culture collection center with the preservation number GDMCC NO:61612. |[0034] 2. Preparation of the culture Medium|[0035] Bacillus brevis v6 activating culture medium (LB liquid medium) comprising tryptone 10g, yeast extract 5g, sodium chloride 10g, distilled water 1000mL, and additional 18g agar for LB solid culture medium;|[0036] The Nitrobacter vickers XY-01 activation medium (HA liquid medium) comprises 2.55g of sodium dihydrogen phosphate, 0.27g of potassium dihydrogen phosphate, l.5g of sodium nitrite, 0.03g of magnesium sulfate, 0.01g of calcium chloride, 0.3g of sodium chloride, 0.03g of ferrous sulfate and 1000mL of distilled water, wherein 18g of agar is additionally added into the HA solid medium; |[0037] the free-living nitrogen fixing bacteria MBC5 activation culture medium (GD liquid culture medium) comprises 0.2g of monopotassium phosphate, 0.2g of magnesium sulfate, 0.2g of sodium chloride, 5g of calcium carbonate, 10g of mannitol, 0.1g of calcium sulfate and 1000mL of distilled water, wherein 20g of agar is additionally added into the GD solid culture medium; |[0038] The active culture medium (YMA liquid culture medium) of the rhizobium slowness Qian2 comprises 0.5g of dipotassium hydrogen phosphate, 0.2g of sodium chloride, 0.2g of magnesium sulfate heptahydrate, 0.1g of calcium sulfate, 1g of calcium carbonate, 0.001g of vitamin B, 100mL of yeast juice, 10g of mannitol and distilled water to 1000mL, wherein 18g of agar is additionally added into the YMA solid culture medium. |[0039] 2. Preparation of soil carbon fixing agent|[0040] 1. Preparation of composite microbial inoculum|[0041] (1) Preparation of bacillus brevis v6 microbial inoculum|[0042] Inoculating the strain v6 to an LB solid medium for activation, carrying out purification through 3-4 times of plate streak transfer, inoculating the purified strain into an LB liquid medium according to the inoculum size of 1.5%, and culturing for 4 days at 28 ℃ to obtain the bacillus brevis v6 microbial inoculum.|[0043] (2) Preparation of Nitrobacter vickers XY-01 microbial inoculum|[0044] The strain XY-01 is inoculated on an HA solid culture medium for activation, the purification is carried out through 3-4 times of flat streak transfer, the purified strain is inoculated into an HA liquid culture medium according to the inoculum size of 1.5 percent, and the culture is carried out for 3 days at the temperature of 28 ℃ to obtain the nitrifying bacteria XY-01.|[0045] (3) Preparation of free-living azotobacter MBC5 microbial inoculum|[0046] The strain MBC5 is inoculated on a GD solid culture medium for activation, the purification is carried out by transferring on a solid plate for 3-4 times, the purified strain is inoculated on a GD liquid culture medium according to the inoculum size of 1.5 percent, and the strain is cultured for 3 days at 28 ℃ to obtain the free-living nitrogen-fixing bacteria MBC5 microbial inoculum.|[0047] (4) Preparation of Rhizobium chromenensis Qian2 microbial inoculum|[0048] Strain Qian2 was inoculated onto YMA solid medium for activation, purified by transfer on solid plates 3-4 times, and the purified strain was inoculated into YMA liquid medium at an inoculum size of 1.5% and cultured at 28 ℃ for 5 days to obtain a slow rhizobium Qian2 inoculum.|[0049] Mixing the prepared bacillus brevis v6 microbial inoculum, the nitrifying bacillus XY-01 microbial inoculum, the free-living nitrogen fixing bacterium MBC5 microbial inoculum and the slow rooting tumor fungus Qian2 microbial inoculum according to the volume ratio of 1:1:2:3 to obtain a composite microbial inoculum, and uniformly mixing biochar, straw fragments and the composite microbial inoculum according to the dosage ratio of 5g to 3g to 10mL to obtain the soil carbon fixing agent.|[0050] 3. Loess plateau abandoned land soil carbon fixation capacity improvement test|[0051] 1. Overview of test zone|[0052] The test area is located in the Wuli gulf region (36 DEG 51 '-36 DEG 53' N,109 DEG 20 '-109 DEG 22' E) of Ansai area of Yanan city of Shaanxi province, and the altitude is 1010-1400 m, and belongs to a typical loess hilly and gully area. The area belongs to a moderate temperate zone continental semiarid monsoon climate, the average air temperature is 8.8 ℃ for many years, the average annual evapotranspiration is 1490mm, the average annual rainfall is 505mm, most rainfall is concentrated in 7-9 months, and the rainfall accounts for about 70% of the annual rainfall. The annual average frost free period is about 157d. The soil in the flow area is mainly yellow cotton soil developed from aeolian loess matrix, has loose soil texture, poor erosion resistance and serious water and soil loss. Currently, 184.18hm 2 is a major type of land use in the penta-gulf stream. The method mainly comprises the steps of rotation planting of corns (Zea mays) and millet (SETARIA ITALICA) before the farmland is abandoned, double cropping in one year, extensive farmland management, no fertilization, irrigation mainly depends on rainfall, all overground parts are removed after crops are harvested, 2 times of intertillage are carried out in a growing season, and the depth is 20cm. No artificial interference exists during the period of barren, and vegetation naturally colonizes and grows.|[0053] 2. Test design|[0054] The present invention selects 1 farmland which was abandoned in 1999 as a test land in the five-gulf stream region in 2001, and the area is about 20m x 20m. 12 cells were randomly established within the experimental plot, each cell having an area of 4m by 5m and a spacing of about 5m from each other. The cell adopts a random block design, wherein the group A is carbon fixing agent adding treatment, the group B is plant community structure adjusting treatment, the group AB is interaction treatment between the group A and the group B, the group CK is a control group, no treatment is carried out, and each treatment is repeated for 3 times. The group A cells (A1, A2 and A3) apply the carbon strengthening agent according to the standard of 10 kg/mu each year without other treatment, the group B cells (B1, B2 and B3) adjust the plant community composition every 5 years without other treatment, and the group AB cells (AB 1, AB2 and AB 3) apply the carbon strengthening agent according to the standard of 10 kg/mu each year and adjust the plant community composition every 5 years. All experiments were started in 2002, vegetation surveys were conducted every 5 years for all cells, and soil samples were collected to analyze the change in carbon sequestration capacity of the abandoned land soil.|[0055] 3. Vegetation investigation method|[0056] And carrying out vegetation investigation in a season of 7 months when vegetation grows vigorously. 51 m hand pieces were laid out in total at the four corners and center of each cell for vegetation investigation. The seed names of all plants, the number of all plant species, the total number of plants per plant, and the coverage of each plant within each panel were recorded. The coverage was assessed visually. All investigation was done jointly by both investigators to reduce human error and finally all investigation data were collated for subsequent analysis.|[0057] 4. Soil sample collection and carbon fixation capacity measurement|[0058] 10 Sampling points are selected in each cell according to an S-shaped sampling method, and after surface fallen matters and humus layers are removed, soil drills with the inner diameter of 5cm are used for collecting surface soil samples with the inner diameter of 0-10 cm. 10 samples in the same district are evenly mixed, sieved by a sieve of 2mm, put into a self-sealing bag and placed into a portable refrigerator for transportation back to a laboratory. The soil sample is divided into two parts, one part is naturally air-dried, and the other part is stored at 4 ℃ and used for the subsequent analysis of the carbon fixing capacity of the soil. In addition, 3 soil sections are randomly selected in each district, and a ring cutter with the volume of 100cm 3 is used for collecting surface layer undisturbed soil samples with the volume of 0-10cm for measuring the soil volume weight.|[0059] Soil organic carbon reserves (Soil organic carbon stock, SOCs) and soil active organic carbon components and refractory organic carbon components are selected to represent the carbon fixing capacity of the soil. Wherein the soil-active organic carbon component comprises microbial biomass carbon (Microbial biomass carbon, MBC), readily oxidizable organic carbon (PERMANGANATE OXIDATIVE ORGANIC CARBON, POXC) and particulate organic carbon (Particulate organic carbon, POC), representing the physical, chemical and biological components of the soil-active organic carbon, respectively, and further wherein the refractory organic carbon component is represented by soil-inert organic carbon (RECALCITRANT ORGANIC CARBON, ROC). The measurement and calculation methods of the above-mentioned index are as follows.|[0060] The organic carbon (Soil organic carbon, SOC) content of the soil is measured by adopting a potassium dichromate-concentrated sulfuric acid external heating capacity method. The soil volume weight is measured by adopting a drying method, namely, a soil sample in the cutting ring is dried to constant weight at 105 ℃, and the dried soil weight per unit cutting ring volume is calculated by weighing to obtain the soil volume weight. Soil organic carbon reserves are calculated according to the following formula:|[0061] SOCS=SOC x D x BD x K|[0062] Wherein SOCs is soil organic carbon reserve (kg/m 2), SOC is soil organic carbon content (g/kg), D is soil thickness (cm), BD is soil volume weight (g/cm 3), and K is a constant of 0.01. |[0063] The carbon (MBC) content of the soil microorganisms is measured by a chloroform fumigation extraction method. 20g of soil samples stored in duplicate at 4℃were weighed into petri dishes, one for chloroform fumigation and the other for no fumigation. The fumigated soil was placed in a desiccator with 5 beakers at the bottom, two of which were each charged with 30mL of chloroform, the other two beakers were charged with 30mL of distilled water, and the last beaker was charged with 30mL of 0.5mol/L sodium hydroxide solution to absorb CO 2 released from the soil. The non-fumigated soil sample was placed in a desiccator with 3 beakers at the bottom, wherein 30mL of distilled water was added to each of the two beakers, and the other 30mL of 0.5mol/L sodium hydroxide solution was added. The desiccator was evacuated and placed in a 25℃incubator for dark culture for 24h. After the cultivation, 12.5g of fumigated and unfused soil samples were weighed and placed in 100mL Erlenmeyer flasks, respectively, 50mL of 0.5mol/L potassium sulfate solution was added, followed by shaking on a 25℃shaker for 30min (200 rpm/min). After filtration, the carbon content in the solution is measured by using an Shimadzu TOC instrument, and the MBC content is the difference value of the carbon content of fumigated and unfused soil samples.|[0064] The content of the easily-oxidizable organic carbon (POXC) in the soil is measured by adopting a potassium permanganate oxidation colorimetric method. 6-10g of air-dried soil samples (ensuring that the carbon content of each sample is in the range of 15-30 mg) were weighed into 50mL centrifuge tubes and used as a blank (no soil sample added). 25mL of 333mmol/L potassium permanganate solution was added, mixed well and placed on a 25℃shaker and shaken for 1h (250 rpm/min). After completion, the tube was centrifuged in a centrifuge at 4800rpm/min for 5 minutes, and the supernatant was diluted 1000/3 times with ultrapure water, and the absorbance of the diluted solution was measured at 565nm with a spectrophotometer. 1mmol/L of potassium permanganate consumes 9mg of carbon in the oxidation process, and the amount of consumed potassium permanganate is calculated according to the difference between the absorbance values of the blank control and the sample solution, so that the POXC content is calculated.|[0065] The organic carbon (POC) content of the soil particles is measured by adopting a sodium hexametaphosphate extraction method. Weighing 20g of air-dried soil sample, placing the air-dried soil sample in a 250mL conical flask, adding 60mL of 5g/L sodium hexametaphosphate solution, shaking the flask by hands for 10-15min, placing the flask on a shaking table for dispersing for 18h (18 ℃ and 90 rpm/min), sieving the dispersion liquid with a 53 mu m sieve, washing the solution with ultra-pure water until the water below the sieve is clear, placing the upper part of the sieve into a granular organic matter, drying the granular organic matter at 80 ℃ for 24h, weighing and calculating the percentage of the granular organic matter in the soil. Grinding the dried granular organic matters, sieving with a 0.149mm sieve, taking a certain weight of the granular organic matters, measuring the carbon content of the granular organic matters by using a potassium dichromate-concentrated sulfuric acid external heating capacity method, multiplying the carbon content by the percentage of the soil, and calculating the POC content.|[0066] The inert organic carbon (ROC) content of the soil is determined by a hydrochloric acid digestion method. 2g of the air-dried soil sample passing through a 1mm sieve is weighed and placed in a 100mL digestion tube, 5mL of 6mol/L hydrochloric acid solution is added and digested for 16h at 125 ℃. The digested soil sample was transferred to a 50mL centrifuge tube, 30mL distilled water was added, shaken vigorously, and centrifuged for 3min in a 4000rpm/min centrifuge. The supernatant was removed, 30mL of distilled water was again added, and the above procedure was repeated 5 times until the hydrochloric acid was thoroughly washed. The cleaned soil sample was dried at 55 ℃ and then assayed for ROC content using potassium dichromate-concentrated sulfuric acid external heating capacity.|[0067] 5. Plant community composition of control group (CK) and soil carbon fixation capacity change|[0068] According to the above-mentioned vegetation investigation method and soil index measurement method, the plant community group (tables 1 and 2) and the soil carbon fixation ability change (shown in Table 3) of the control abandoned land were examined in 2002-2022.|[0069] Table 1 changes in plant population composition in control plots 2002-2007|[0070] |[0071] |[0072] |[0073] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0074] Table 2 2012-2022 changes in plant population composition in control plots|[0075] |[0076] |[0077] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0078] Table 3 changes in soil carbon sequestration Capacity in the control group of 2002-2022 abandoned lands|[0079] |[0080] Note that the data are mean ± standard error, and that the same column of different lower case letters indicates significant differences between different years (P < 0.05).|[0081] The results shown in tables 1 and 2 demonstrate that in 2002-2022, 56 plants were counted in the control group cells and were belonging to 22 families, 6 of gramineae, 4 of leguminous plants and 18 of Compositae. On average, the densities of Gramineae, leguminosae and Compositae were 11.80 strain/m 2, 0.83 strain/m 2 and 21.38 strain/m 2, respectively, and the coverage was 17.65%, 1.94% and 35.01%, respectively. The density and coverage of gramineae and leguminous plants tended to increase during the test period, but the gramineae was not significantly increased, and the overall density and coverage were not high despite the tremendous increase in leguminous plants.|[0082] The contribution of three grasses, such as mesona, oak and Cryptocarya, to the density and coverage of the community of the plant in the barren land increases year by year, increasing from 0.48% and 1.11% in 2002 (density contribution) to 23.60% and 31.14% in 2022, respectively, and likewise, the contribution of three leguminous plants, such as Pisum album, astragalus trifoliatus and Lespedeza multiflora, to the density and coverage of the community of the plant in the barren land increases year by year, increasing from 0% and 0% in 2002 to 2.89% and 5.47% in 2022, respectively. In addition, the contributions of the three kinds of plants of the asteraceae family, namely the spanishneedles herb, the herba artemisiae capillaris and the herba artemisiae annuae to the community density and the coverage of the abandoned barren land are 22.02-29.32% and 29.16-47.66% respectively, but no obvious annual change trend exists.|[0083] As is clear from Table 3, in 2002-2022, the organic carbon reserves, the microbial carbon, the readily oxidizable organic carbon and the particulate organic carbon contents of the soil increased year by year (P < 0.05), the average increases were 29.55%, 75.90%, 253.33% and 57.82%, respectively, but the inert organic carbon contents of the soil did not change significantly, the average increases during the test were 13.80%, and the above results generally indicate that the soil carbon fixing ability of the control group increased slowly.|[0084] 6. Soil carbon fixation capacity improvement test of abandoned land|[0085] Starting in 2002, carbon fixing agents are spread on the soil surfaces of AB1, AB2 and AB3 cells according to the application amount of 10 kg/mu every year, and plant community structures are adjusted once in 2002, 2007, 2012, 2017 and 2022 respectively.|[0086] The specific implementation process of the plant community structure adjustment is as follows:|[0087] (1) Leguminous and gramineous plant reseeding |[0088] In the test, lespedeza multiflora, astragalus trifolitan, viola yessoensis, cynanchum komarovii and Gramineae are selected and planted in a mixed mode. The sowing quantity of each grass seed in the mixed sowing combination is calculated by the product of the mixed sowing proportion of the grass seed in the mixed sowing combination and the single sowing quantity of the grass seed. Wherein, the unicast amount of the Lespedeza multiflora, the trifolith astragalus root, the field pea, the goose grass, the Phryegrass and the elymus is 5.0 kg/mu, 2.5 kg/mu, 1.5 kg/mu and 2.0 kg/mu respectively. The ratio of bean-grass mixed sowing (mixed sowing of leguminous plants and gramineous plants) is 1:1, and the total sowing amount is 2.5 kg/mu. Thus, the sowing amount of the Lespedeza multiflora, the trifolith astragalus membranaceus, the vetch, the mesona chinensis, the crypt-seed grass and the elymus-cape grass is respectively 0.835 kg/mu, 0.415 kg/mu, 0.25 kg/mu and 0.335 kg/mu when the beans-grass are mixed.|[0089] The 6 grass seeds are fully and uniformly mixed and then soaked in warm water at 45 ℃ for 24 hours, and after soaking, the grass seeds are sown in the same row, each cell is sown in the same row in a supplementary mode, the row spacing is 30cm, and the sowing depth is 2cm. The method comprises the steps of first-time supplementary seeding in 2002, 2007, 2012, 2017 and 2022 respectively, not applying fertilizer, not irrigating and not mowing after seeding, carrying out vegetation investigation in the vegetation growth vigorous period at the end of 7 months in the current year, and collecting soil samples to analyze the carbon fixation capacity of the soil.|[0090] The mesona blume seeds and the cryptopsis subulata seeds are purchased from Jiangsu Xin Rui seed industry Co., ltd, the Alternaria alternata seeds, the Vicia and the Lespedeza multiflora seed seeds are purchased from Jiangsu Gangren Bozier seed industry Co., ltd, and the Daghestan astragalus seed is provided by the grassland research of the national academy of agricultural and animal husbandry of inner Mongolian. The germination rate of all grass seeds is 73% -89%, the water content is 3% -12%, the purity is 80% -90%, and the variety purity is 90% -95%.|[0091] (2) Compositae dominant species removal|[0092] To ensure the removal effect, the removal of the dominant species of the asteraceae plants was completed in the previous year of the leguminous and gramineous plants' complementary sowing, i.e. the whole root of the spanishneedles herb, the artemisia capillaris and the artemisia capillaris in the test cell was removed at the end of 7 months of 2001, 2006, 2011, 2016 and 2021, respectively.|[0093] Meanwhile, in the test communities A1, A2 and A3,2002-2022, the carbon fixing agent is sprayed every year according to the application amount of 10 kg/mu, the plant community composition is not changed artificially, vegetation surveys are respectively carried out at the end of 7 months of 2002, 2007, 2012, 2017 and 2022, and soil samples are collected to analyze the carbon fixing capacity of the soil.|[0094] In addition, for test cells B1, B2 and B3, plant colony structures were adjusted at the beginning of 4 months in 2002, 2007, 2012, 2017 and 2022, respectively, the specific operation was as described above, but no carbon strengthening agent was applied, and vegetation surveys were conducted at the end of 7 months in 2002, 2007, 2012, 2017 and 2022, respectively, and soil samples were collected to analyze soil carbon fixation ability.|[0095] 4. Analysis of experimental results|[0096] 1. Influence of carbon sequestration agent on carbon sequestration capacity of soil in loess plateau|[0097] After applying only the carbon fixing agent, the plant community composition (table 4 and table 5) and the carbon fixing ability change of the soil (as shown in table 6) on the land of the barren lands in 2002, 2007, 2012, 2017 and 2022.|[0098] Table 4 changes in plant community composition in the abandoned lands where the carbon reinforcing agent was applied alone in 2002-2007|[0099] |[0100] |[0101] |[0102] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0103] Table 5 2012-2022 Change in plant community composition of abandoned land with carbon reinforcing agent applied alone|[0104] |[0105] |[0106] |[0107] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0108] As can be seen from tables 4 and 5, in 2002-2022, 62 plants were counted in the cell to which only the carbon strengthening agent was applied, and the plants were classified into 24 families, wherein 6 plants of Gramineae, 5 plants of Leguminosae, and 20 plants of Compositae were counted. On average, the densities of Gramineae, leguminosae and Compositae were 12.23 strain/m 2, 1.26 strain/m 2 and 22.23 strain/m 2, respectively, and the coverage was 20.17%, 2.20% and 33.08%, respectively. Similar to the control group, the density and coverage of both Gramineae and Leguminosae plants tended to increase during the test, but the enhancement of Gramineae was not obvious, and the overall density and coverage were not high despite the tremendous enhancement of Leguminosae plants. In general, the application of the carbon fixing agent increases the species richness of the community of plants in the abandoned land, increases the density of the grasses, legumes and asteraceae plants, increases the coverage of the grasses and legumes, but decreases the coverage of the asteraceae plants.|[0109] Specifically, after the application of the carbon fixing agent, the contribution of three grasses of the order Centipeda minima, oak and Cryptotaea has been increased year by year from 3.61% (density contribution) and 4.28% (coverage contribution, the same applies hereinafter) in 2002 to 23.84% and 31.87% in 2022, respectively, and the contribution of three leguminous plants of the order Daphne, astragalus trifoliatus and Lespedeza multiflora to the plant community density and coverage has also been increased year by year from 1.22% and 1.35% in 2002 to 4.39% and 4.24% in 2022, respectively. In addition, the contributions of the three kinds of plants of the asteraceae family, namely the spanishneedles herb, the herba artemisiae capillaris and the herba artemisiae annuae to the community density and the coverage of the abandoned barren land are respectively 15.01-36.33% and 17.56-34.28%, and the obvious annual change trend does not exist.|[0110] Compared with the control group, the application of the carbon strengthening agent improves the density of gramineae, leguminous and Compositae plants by 3.73 percent, 74.42 percent and 4.37 percent on average, and improves the density of the three gramineae plants, the three leguminous plants and the three Compositae plants by 212.86 percent, 91.64 percent and 5.11 percent on average compared with the control group. In addition, the application of the carbon fixing agent increases the coverage of gramineae and leguminous plants by 17.31% and 104.31% respectively compared with the control group, but reduces the coverage of Compositae plants by 4.95% compared with the control group, and likewise, the application of the carbon fixing agent increases the coverage of the three gramineae plants and the three leguminous plants by 192.03% and 221.01% respectively compared with the control group, but reduces the coverage of the three Compositae plants by 19.30% compared with the control group.|[0111] Table 6 changes in carbon sequestration Capacity of the abandoned land soil with only carbon sequestrants applied in 2002-2022|[0112] |[0113] Note that the data are mean ± standard error, and that the same column of different lower case letters indicates significant differences between different years (P < 0.05).|[0114] The results shown in Table 6 demonstrate that in 2002-2022, the soil organic carbon reserves, microbial carbon, readily oxidizable organic carbon and particulate organic carbon content of the carbon-reinforcing agent cells were only increased year by year (P < 0.05), with average increases of 58.33%, 105.24%, 177.27% and 30.32%, respectively, and the soil inert organic carbon content was not significantly changed, with average increases of 21.64% during the test. In addition, the application of the carbon fixing agent increases the carbon fixing capability index of the 5 soil by 86.74%, 25.31%, 28.57%, 21.30% and 13.12% respectively compared with the control group, which indicates that the carbon fixing capability of the abandoned land soil can be improved to a certain extent by only applying the carbon fixing agent.|[0115] 2. Regulating influence of plant community structure on carbon fixation capacity of loess plateau abandoned land soil|[0116] Changes in carbon sequestration capacity of soil after adjustment of plant community species composition alone on the lands of the barren lands 2002, 2007, 2012, 2017 and 2022 are shown in tables 7 and 8, respectively.|[0117] Table 7 2002-2007 changes in plant community composition of the abandoned land for which plant community structure was adjusted only|[0118] |[0119] |[0120] |[0121] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0122] Table 8 2012-2022 changes in plant community composition of the abandoned land for plant community structure adjustment only|[0123] |[0124] |[0125] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0126] As is clear from tables 7 and 8, in 2002-2022, the total statistics of 55 plants in the cell with the plant community structure were adjusted to be 21 plants, wherein 9 plants of Gramineae, 6 plants of Leguminosae and 15 plants of Compositae were used. On average, the densities of Gramineae, leguminosae and Compositae were 16.47 strain/m 2, 9.69 strain/m 2 and 14.65 strain/m 2, respectively, and the coverage was 35.84%, 20.83% and 17.69%, respectively. The density and coverage of each of the Gramineae, leguminosae and Compositae plants are not greatly changed with time due to the regular adjustment of the plant community composition, but compared with the control group, the adjustment of the plant community structure obviously improves the species uniformity of the plant community in the abandoned lands, increases the density and coverage of the Gramineae and Leguminosae plants, and reduces the density and coverage of the Compositae plants.|[0127] Specifically, after plant community structure is adjusted, the contribution of three grasses of herba chenopodii, herba Oenotherae Erythrosepalae and Cryptotaenia japonica to the community density and coverage of the abandoned barren land is 26.90% -28.90% and 35.17% -42.58%, the contribution of three leguminous plants of herba Violae, radix astragali Melilotoidis and Lespedeza multiflora to the community density and coverage of the abandoned barren land is 16.03% -18.50% and 20.94% -28.02%, and the contribution of three kinds of plants of the Compositae of herba Bidentis Bipinnatae, herba Artemisiae Scopariae and herba Artemisiae Scopariae to the community density and coverage of the abandoned barren land is 4.58% -12.06% and 2.89% -11.35%, respectively, and no obvious annual change trend is shown.|[0128] Compared with the control group, the density of the gramineae and leguminous plants is improved by 40.43 percent and 1665.89 percent respectively by adjusting the plant community structure, and the density of the three gramineae plants and the three leguminous plants is improved more than that of the control group, and the increase of the gramineae plants and the leguminous plants is 1778.85 percent and 1897.08 percent respectively. In addition, the plant community structure is adjusted to increase the coverage of gramineae and leguminous plants by 125.95% and 2358.63% respectively compared with the average coverage of the control group, and the coverage of the three gramineae plants and leguminous plants is increased by 1920.01% and 5010.22% respectively compared with the average coverage of the control group. In contrast, after plant colony structure was adjusted, the densities and coverage of the asteroid plants were reduced by 30.38% and 48.89% respectively compared to the control group, and in particular, the densities and coverage of the three asteroid plants were reduced by 64.47% and 76.55% respectively compared to the control group.|[0129] Table 9 2002-2022 changes in carbon sequestration ability of the soil of abandoned lands in which plant colony structures were regulated alone|[0130] |[0131] Note that the data are mean ± standard error, and that the same column of different lower case letters indicates significant differences between different years (P < 0.05).|[0132] As can be seen from Table 9, after the plant community structure was adjusted, the average increases in soil organic carbon reserves, microbial biomass carbon, readily oxidizable organic carbon, particulate organic carbon and inert organic carbon content were 20.69%, 115.31%, 211.11%, 108.97% and 9.52%, respectively, over the year 2002-2022, and although the various indices characterizing the soil carbon fixing ability generally tended to increase over time, the differences in soil organic carbon reserves and inert organic carbon content did not reach significant levels over the different years. In addition, the plant community structure is adjusted to ensure that the organic carbon reserves, the microbial biomass carbon, the easily oxidized organic carbon and the inert organic carbon content of the soil are respectively increased by 25.89%, 6.88%, 14.00% and 2.16% compared with the control group, but the organic carbon content of soil particles is reduced by 28.44% compared with the control group, and the result shows that the carbon fixing capability of the soil in the barren lands can be improved to a certain extent by only adjusting the plant community structure, but the effect is lower than that of the treatment by only applying the carbon fixing agent.|[0133] 3. The invention has the effect on the carbon fixation capacity of the soil of the loess plateau abandoned barren land|[0134] The changes in the carbon sequestration ability of the soil after applying the carbon sequestration agent and adjusting the plant community structure on the land of the barren lands 2002, 2007, 2012, 2017 and 2022 are shown in tables 10 and 11, respectively.|[0135] Table 10 2002-2007 changes in the composition of the plant communities of the abandoned land in which the present invention was practiced|[0136] |[0137] |[0138] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0139] Table 11 2012-2022 Change in plant community composition in the abandoned land where the invention was practiced|[0140] |[0141] |[0142] Note that the data are mean ± standard error, "-" indicates that no such plant species is present in the abandoned lands of the corresponding year.|[0143] As is clear from tables 10 and 11, in 2002-2022, 59 plants were counted in the cell in which the present invention was practiced, and the plants were belonging to 23 families, wherein 10 plants of Gramineae, 9 plants of Leguminosae, and 15 plants of Compositae. On average, the densities of the gramineae, leguminous and asteraceae plants were 17.10 strain/m 2, 9.78 strain/m 2 and 13.47 strain/m 2, respectively, with coverage levels of 35.40%, 20.66% and 19.16%, respectively. After the invention is implemented, the density and coverage of the gramineae, leguminous and asteraceae plants are not greatly different from those of the cells with the structure of the plant community, but compared with the control group and the application of the carbon strengthening agent, the invention obviously improves the species uniformity of the plant community of the barren lands, increases the density and coverage of the gramineae and leguminous plants, and reduces the density and coverage of the asteraceae plants.|[0144] Specifically, after the invention is implemented, the contributions of three gramineous plants of herba chenopodii, herba Oenotherae Erythrosepalae and cryptotaenia japonica to the community density and coverage of the abandoned lands are 24.29% -34.16% and 32.97% -41.85%, the contributions of three leguminous plants of herba Violae, radix astragali and Lespedeza multiflora to the community density and coverage of the abandoned lands are 16.00% -18.94% and 14.93% -25.91%, and the contributions of three kinds of plants of the jektight, herba Artemisiae Scopariae and herba Artemisiae Scopariae to the community density and coverage of the abandoned lands are 3.13% -10.93% and 2.22% -6.22%, respectively, and the obvious annual change trend is not shown.|[0145] Compared with the control group, the density of the gramineae and the leguminous plants is averagely improved by 45.70 percent and 1672.06 percent, the density of the gramineae and the leguminous plants is improved by more than 1895.93 percent and 2000.47 percent compared with the control group, and the coverage of the gramineae and the leguminous plants is averagely improved by 122.72 percent and 2465.90 percent compared with the control group, and the coverage of the gramineae and the leguminous plants is improved by 1859.14 percent and 6167.90 percent compared with the control group. In contrast, the densities and coverage of the asteraceae plants were reduced by 36.04% and 44.87% on average, respectively, compared to the control group, and the densities and coverage of the three asteraceae plants were reduced by 70.46% and 86.07% on average, respectively.|[0146] Table 12 2002-2022 Change in the carbon sequestration Capacity of the soil in the abandoned land where the invention was practiced|[0147] |[0148] |[0149] Note that the data are mean ± standard error, and that the same column of different lower case letters indicates significant differences between different years (P < 0.05).|[0150] As can be seen from table 12, the carbon fixing agent was applied while adjusting the plant community structure to significantly improve the soil carbon fixing ability of the abandoned lands, and the average increases in the soil organic carbon reserves, microbial carbon, readily oxidizable organic carbon, particulate organic carbon and inert organic carbon content between 2002-2022 were 66.67%, 148.00%, 169.23%, 77.48% and 34.81%, respectively (P < 0.05). Compared with a control group, the method ensures that the indexes for representing the soil carbon fixing capacity of the 5 indexes are respectively increased by 153.38%, 47.45%, 51.93%, 17.39% and 17.85% compared with the average indexes of the control group, and the results of different treatments show that the method has the best effect of improving the soil carbon fixing capacity.|[0151] 4. Effect contrast of improving carbon fixation capacity of soil of abandoned wasteland by different treatments|[0152] Table 13 2002-2022 comparison of soil carbon sequestration improvement effects for different treatments compared to control group|[0153] |[0154] |[0155] Note that the data are mean ± standard error.|[0156] Table 13 shows the increase in carbon sequestration capacity of the barren land soil over the control group in 2002, 2007, 2012, 2017 and 2022 after applying only the carbon sequestration agent, adjusting only the plant community structure and practicing the invention. It can be seen that:|[0157] (1) In addition, the invention can improve the carbon fixation capacity of soil by only applying the carbon strengthening agent and only adjusting the plant community structure, but the effect is obviously lower than that of the invention, and particularly, the invention can improve the organic carbon reserves, the microbial carbon content, the easily-oxidizable organic carbon content and the inert organic carbon content of soil by 1.77 times, 1.80 times, 1.79 times and 1.35 times of the effect of only applying the carbon strengthening agent respectively on average and 5.84 times, 5.39 times, 2.75 times and 6.02 times of the effect of only adjusting the plant community structure respectively. |[0158] (2) In 2002-2022, the invention can respectively and averagely increase the organic carbon reserves, the microbial carbon content, the easily-oxidized organic carbon content, the granular organic carbon content and the inert organic carbon content by 152.84 percent, 49.98 percent, 67.96 percent, 18.00 percent and 19.45 percent, particularly, the indexes 5 can respectively increase 126.67 percent, 13.70 percent, 82.91 percent, 3.10 percent and 10.57 percent in the current year of the invention, and the lifting effect is in an overall year-by-year increasing trend, which indicates that the invention can rapidly, effectively and continuously improve the carbon fixing capability of the soil of the loess plateau and the barren land, and can be popularized and applied.|[0159] While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the following claims be interpreted as including the preferred embodiments and all such alterations and modifications as fall within the scope of the invention.|[0160] It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof. Family Number|(105745947)|105745947|Abstract|(CN116420457B B)|The invention relates to the technical field of carbon sequestration , and particularly discloses a method for improving the soil carbon sequestration capacity of abandoned land of loess plateau , which comprises the steps of carbon sequestration agent preparation and plant community structure adjustment . The carbon sequestration agent is prepared from biochar , crushed straw and a complex microbial inoculant according to the dosage ratio of ( 4-6 ) g : ( 2-3 ) g : ( 6-10 ) mL . The complex microbial inoculant is prepared by mixing nitrified brevibacillus vv6 , nitrobacter winogradsky XY - 01, authigenic nitrogen - fixing bacteria MBC5 and bradyrhizobium Qian2 according to the volume ratio of 1 : 1 : ( 2-3 ) : ( 2-4 ) ; the plant community structure adjustment comprises reseeding indigenous leguminous plants and gramineous plants , and reducing the number of dominant species of compositae plants . By applying the carbon reinforcing agent and optimizing the plant community , the carbon sequestration capability of the abandoned land soil of the loess plateau can be remarkably improved , and the method has important practical significance for building a carbon sequestration and sink increasing type vegetation restoration ecological system and assists an ecological environment fragile area to achieve the dual - carbon target . |CPC codes|(CN116420457B B)|A01B - 079/02 |A01G - 022/00 |IPC codes|(CN116420457B B)|A01B - 079/02 |A01G - 022/00 |Title|(CN116420457 A)|Method for improving carbon sequestration capacity of soil of abandoned land of loess plateau | Basic materials chemistry|Biotechnology|Other special machines A01B-079/02|A01G-022/00|C09K-017/40|C12N-001/20|C12R-2001/01|C12R-2001/41 A01B-079/02|A01G-022/00|C09K-017/40|C12N-001/20|C12R-2001/01|C12R-2001/41 A01B-079/02|A01G-022/00|C09K-017/40|C12N-001/20|C12R-001/01|C12R-001/41 A01B-079/02|A01G-022/00|C09K-017/40|C12N-001/20|C12R-001/01|C12R-001/41 CN119220437|CN118584836|CN118130409 CN119220437 112861186 WHO=Examiner SELF=N CAT=A|CN118584836 111305886 WHO=Examiner SELF=N CAT=A|CN118130409 110039961 WHO=Examiner SELF=N CAT=A CN115921521|CN115553174|CN115846395|CN115462289|CN110183272|EP3085679|CN108624528|CN104488396 CN115921521 104481589 WHO=Examiner SELF=N CAT=A|CN115553174 103264103 WHO=Examiner SELF=N CAT=A|CN115846395 104324454 WHO=Examiner SELF=N CAT=A|CN115462289 102975184 WHO=Examiner SELF=N CAT=A|CN110183272 85847457 WHO=Examiner SELF=N CAT=A|EP3085679 74460339 WHO=Examiner SELF=N CAT=A|CN108624528 81577586 WHO=Examiner SELF=N|CN104488396 69001045 WHO=Examiner SELF=N EP3085679; CN110183272; CN115462289; CN115553174; CN115846395; CN115921521; CN104488396; CN108624528 GRANTED (CN116420457)|GRANTED ALIVE (CN116420457)|ALIVE (CN116420457)|LEGAL DETAILS FOR CN116420457|Actual or expected expiration date=2043-04-13|Legal state=ALIVE|Status=GRANTED|Event publication date=2023-04-13|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202310394318|Application date=2023-04-13|Standardized application number=2023CN-0394318|Event publication date=2023-07-14|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN116420457|Publication stage code=A|Publication date=2023-07-14|Standardized publication number=CN116420457|Event publication date=2023-07-14|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-08-01|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-05-06|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN116420457|Publication stage code=B|Publication date=2025-05-06|Standardized publication number=CN116420457B|Event publication date=2025-05-06|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN116420457)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSoLhFWwh+boxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000077387400&ekey=1794&xpn=CN116420457B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=GT7d%252FXkEtrVji4lOmRkQm7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN116420457)|CN|(CN116420457)|CN (CN116420457)|NAME=NORTHWEST SCI-TECH UNIVERSITY OF AGRICULTURE & FORESTRY , COUNTRY=CN|(CN116420457)|NAME=NORTHWEST SCI-TECH UNIVERSITY OF AGRICULTURE & FORESTRY , COUNTRY=CN (CN116420457)|NAME=CUI RUIYING;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223|(CN116420457)|NAME=CUI RUIYING;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223 (CN116420457)|NAME=ZHONG ZEKUN|NAME=WANG XING|NAME=WANG YONGLIANG|NAME=REN CHENGJIE|NAME=HAN XINHUI|NAME=YANG GAIHE|(CN116420457)|NAME=ZHONG ZEKUN|NAME=WANG XING|NAME=WANG YONGLIANG|NAME=REN CHENGJIE|NAME=HAN XINHUI|NAME=YANG GAIHE 0 1 Titre: (CN116420457)|Method for improving carbon fixation capacity of soil of loess plateau abandoned wasteland Résumé: (CN116420457)|The invention relates to the technical field of carbon sequestration, and particularly discloses a method for improving the soil carbon sequestration capacity of abandoned land of loess plateau, which comprises the steps of carbon sequestration agent preparation and plant community structure adjustment. The carbon sequestration agent is prepared from biochar, crushed straw and a complex microbial inoculant according to the dosage ratio of (4-6) g: (2-3) g: (6-10) mL. The complex microbial inoculant is prepared by mixing nitrified brevibacillus vv6, nitrobacter winogradsky XY-01, authigenic nitrogen-fixing bacteria MBC5 and bradyrhizobium Qian2 according to the volume ratio of 1: 1: (2-3): (2-4); the plant community structure adjustment comprises reseeding indigenous leguminous plants and gramineous plants, and reducing the number of dominant species of compositae plants. By applying the carbon reinforcing agent and optimizing the plant community, the carbon sequestration capability of the abandoned land soil of the loess plateau can be remarkably improved, and the method has important practical significance for building a carbon sequestration and sink increasing type vegetation restoration ecological system and assists an ecological environment fragile area to achieve the dual-carbon target. 65 Abstract gpt-4o-mini no The article focuses on improving soil carbon sequestration using biochar and microbial inoculants, without addressing the accelerated weathering of minerals or CO₂ capture through mineral carbonation.
66 CN202411116320 CN202411116320 CN119076589 112511768 CN119076589 A 2024-12-06 [CN119076589] 2024-08-14 2024-08-14 2024-12-06 (CN119076589)|2044-08-14 (CN119076589)|Method for cooperatively weathering gas and phosphate tailings into soil (CN119076589)|The invention discloses a method for synergistically weathering gas and phosphate tailings into soil. The method comprises the following steps: firstly, preparing phosphate tailings into granular filler, loading methane-oxidizing bacteria on the granular filler, and constructing a biological filter bed which takes phosphate tailings particles as a biofilm carrier and takes the methane-oxidizing bacteria as dominant microorganisms; gas is introduced into the biological filter bed, the concentration of methane in the gas is 0.1%-30% by volume, methane in the gas is biologically oxidized by methane-oxidizing bacteria, mineral decomposition and reconstruction of phosphate tailing particles are accelerated by methane metabolites, available phosphorus components are released, and weathered products are obtained. According to the method, organic acid produced by biochemical degradation of methane through methane-oxidizing bacteria is utilized, decomposition reconstruction and weathering stabilization of various minerals in the phosphate tailings are accelerated, activation and release of phosphate fertilizer in the phosphate tailings are promoted, organic matter conversion of methane in weathered products is achieved, finally, biological carbon sequestration of methane and the phosphate tailings are rapidly weathered into soil, and the phosphorus tailings are rapidly decomposed into soil. Co-processing and recycling of the gas and the phosphate tailings are realized. KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY (CN119076589)|KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) HU XUEWEI|YANG YANG|SONG HAORAN|ZHAO QUN|TIAN SENLIN|ZHANG QING (CN119076589)|HU XUEWEI|YANG YANG|SONG HAORAN|ZHAO QUN|TIAN SENLIN|ZHANG QING (CN119076589)|ZHANG YANG;Kunming Tongju Patent Agency Co., Ltd.|Reg. Nb: 53214|ZHANG YU;Kunming Tongju Patent Agency Co., Ltd.|Reg. Nb: 53214 (CN119076589)|For this reason, it is necessary to develop a method for the synergistic weathering of gas and phosphate tailings into soil which can solve the above problems.|The prior art is used for treating and recycling the phosphate tailings, because the physical separation method is dependent on gravity, magnetism or floatation and other principles, and can require complex equipment and operation, so that the treatment cost is high, and because the chemical treatment method involves changing the chemical property in the tailings by an extraction-back extraction method, a carbonization method or a calcination-leaching method, harmful substances can be introduced or waste water which is difficult to treat is generated, so that the environmental pollution risk is high.| (CN119076589)|1. The method for forming soil by the synergistic weathering of the gas and the phosphate tailings is characterized by comprising the following steps: S1, preparing phosphate tailings into particle filler, loading methane-oxidizing bacteria on the particle filler, and constructing a biological filter bed which takes phosphate tailings particles as a biological membrane carrier and methane-oxidizing bacteria as dominant microorganisms; S2, introducing gas into the biological filter bed, wherein the methane concentration in the gas is 0.1-30% by volume, the methane in the gas is biologically oxidized by methane oxidizing bacteria, and methane metabolites accelerate the mineral decomposition and reconstruction of the phosphate tailing particles, so that effective phosphorus components are released, and a weathered product is obtained. | (CN119076589)|The invention aims to provide a method for forming soil by the synergistic weathering of methane and phosphate tailings, which utilizes organic acid produced by methane biochemical degradation of methane by methane oxidizing bacteria to accelerate decomposition, reconstruction and weathering stabilization of various minerals in the phosphate tailings, promote activation and release of phosphate fertilizer in the phosphate tailings, realize organic matter conversion of methane in weathered products, finally realize rapid weathering of biological carbon fixation of the methane and the phosphate tailings into soil, and realize synergistic treatment and recycling of the methane and the phosphate tailings.The object of the invention is achieved in that it comprises the following steps:|The invention discloses a method for forming soil by synergistic weathering of gas and phosphate tailings, which comprises the steps of firstly preparing phosphate tailings into particle fillers, loading methane oxidizing bacteria on the particle fillers, constructing a biological filter bed which takes phosphate tailings particles as a biological membrane carrier and takes methane oxidizing bacteria as dominant microorganisms, introducing the gas into the biological filter bed, wherein the methane concentration in the gas is 0.1-30% by volume, and the methane in the gas is biologically oxidized by the methane oxidizing bacteria, so that methane metabolites accelerate the mineral decomposition reconstruction of the phosphate tailings particles, and release effective phosphorus components, thereby obtaining weathered products.| (CN119076589)|PHOSPHATE TAILING(100,60)|GROUND(100,23)|SYNERGISTIC WEATHERING(100,14)|GAS SYNERGISTIC WEATHERING(100,13)|METHANE OXIDIZING BACTERIUM(93,38)|OXIDIZING BACTERIA(67,13)|METHANE SYNERGISTIC WEATHERING(46,1)|METHANE BIOCHEMICAL DEGRADATION(44,2)|DOMINANT MICROORGANISM(42,4)|PARTICLE FILLER(41,10)|METHANE METABOLITE(39,4)|MINERAL DECOMPOSITION RECONSTRUCTION(38,2)|MINERAL STABILIZATION(35,2)|LOADING METHANE OXIDIZING BACTERIUM(33,3)|PHOSPHATE FERTILIZER(32,2)|ACCELERATE DECOMPOSITION RECONSTRUCTION(32,1)|BIOCHEMICAL DEGRADATION(31,2)|BIOLOGICAL FILTER BED(30,9)|DECOMPOSITION ACCELERATOR(26,1)|PHOSPHATE TAILING PARTICLE(24,4)|SYNERGISTIC TREATMENT(24,2)|WEATHERED PRODUCT(23,13)|SUBTYPE IB BACTERIUM(23,3)|MINERAL DECOMPOSITION(23,2)|METHANE(22,23)|BIOLOGICAL MEMBRANE CARRIER(22,3)|HARMFUL SUBSTANCE(22,1)|PHOSPHORUS COMPONENT(21,4)|RAPID WEATHERING(21,1)|GRANULAR FILLER(20,5)|TAILING PARTICLE(19,4)|RECONSTRUCTION(19,3)|ENVIRONMENTAL POLLUTION RISK(19,1)|METHANE ORGANIC MATTER CONVERSION(17,2)|CALCINATION LEACHING(17,1)|CARBONIZATION(17,1)|LIQUID INTERMITTENT INFILTRATION(17,1)|TAILING(16,4)|BIOLOGICAL MEMBRANE(16,3)|METHYL MICROZYME(15,1)|METHYL CAMPYLOBACTER(14,2)|FLOATATION(14,1)|WASTEWATER(14,1)|MAGNETIC FORCE(13,1)|METHYL SARCINA(12,3)|ORGANIC MATTER CONVERSION(12,2)|COMPLEX EQUIPMENT(12,1)|ENVIRONMENTAL POLLUTION(12,1)|LIQUID CONTINUOUS CIRCULATION LEACHING(12,1)|MINERAL SEPARATION(12,1)|METHYL MONAD(11,4)|METHANE CARBON FIXATION(11,2)|WEATHERING PRODUCT(11,2)|METHANE OXIDIZING BACTERIUM PROLIFERATION(10,2)|BINDER(9,4)|CARBON FIXATION(9,4)|MOLDING PRESS(9,2)|METHYLOCOCCUS(8,11)|GRANULATOR(8,2)|BENTONITE(7,4)|ECOLOGICAL MATRIX SOIL(7,3)|TAILING LEFT(7,3)|CHEMICAL PROPERTY(7,1)|METHANE OXIDIZING BACTERIUM METABOLITE(7,1)|METHYLCYST BACTERIUM FLORA(7,1)|BIOCATALYTICALLY OXIDIZE METHANE(6,1)|SODIUM SILICATE(5,3)|WEATHERED PRODUCT AGGLOMERATION(5,2)|ORGANIC ACID(4,7)|BACTERIUM LIQUID(4,6)|EXTRACELLULAR POLYMER(4,3)|ALUMINUM DIHYDROGEN PHOSPHATE(4,2)|CONCENTRATE EXTRACTION(4,2)|SOIL MOISTURE CONSERVATION(4,2)|BACTERIUM BIOLOGICAL OXIDATION METHANE(4,1)|DECOMPOSITION RECONSTRUCTION(4,1)|LEACHING CIRCULATION(4,1)|METHYL BACILLUS BACTERIUM(4,1)|METHYLOBACTERIUM POPULATION(4,1)|TREATMENT COST(4,1)|WASTE RESOURCE UTILIZATION(4,1)|WEATHERING DECOMPOSITION(4,1)|METHYLOMONAS(3,5)|METHYLOSINUS(3,3)|FERTILIZER STORAGE PERFORMANCE(3,2)|APATITE PHOSPHATE(3,1)|DISSOLUBLE MICROORGANISM PRODUCT(3,1)|EARTH RESOURCE(3,1)|SILICATE MINERAL RECONSTRUCTION(3,1)|CARBONATE MINERAL(2,1)|ECOLOGICAL ENVIRONMENT(2,1)|GRAIN SIZE(2,1)|METHYL COCCI(2,1)|METHYL COCCUS(2,1)|METHYL CYSTOMYCETE(2,1)|METHYL GROUP MICROORGANISM(2,1)|METHYL MICROCOCCUS(2,1)|PHOSPHATE MINERAL(2,1)|PHOSPHATE ORE(2,1)|RESOURCE WASTE(2,1)| (CN119076589)|1. The method for forming soil by the synergistic weathering of the gas and the phosphate tailings is characterized by comprising the following steps:| S1, preparing phosphate tailings into particle filler, loading methane-oxidizing bacteria on the particle filler, and constructing a biological filter bed which takes phosphate tailings particles as a biological membrane carrier and methane-oxidizing bacteria as dominant microorganisms; | S2, introducing gas into the biological filter bed, wherein the methane concentration in the gas is 0.1-30% by volume, the methane in the gas is biologically oxidized by methane oxidizing bacteria, and methane metabolites accelerate the mineral decomposition and reconstruction of the phosphate tailing particles, so that effective phosphorus components are released, and a weathered product is obtained. |2. The method for the synergistic weathering of gas and phosphate tailings into soil according to claim 1, wherein the methane-oxidizing bacteria comprise one or more of methylobacterium, methylococcus, methyl monad, methyl microzyme, methyl sarcina, methyl campylobacter, methyl cysts and subtype Ib bacteria.|3. The method for the synergistic weathering of gas and phosphate tailings into soil according to claim 1, wherein the phosphate tailings are tailings left after concentrate extraction by mineral separation.|4. The method for forming soil by co-weathering gas and phosphate tailings according to claim 1, wherein before the step S1 is performed to form the particle filler, a binder is added to the phosphate tailings and uniformly mixed, and the binder comprises one or more of bentonite, sodium silicate and aluminum dihydrogen phosphate.|5. The method for forming soil by synergistic weathering of gas and phosphate tailings according to claim 1, wherein the step S1 is characterized in that the granular filler is obtained by pressing the phosphate tailings through a granulator or a molding press and then sintering the phosphate tailings, and the grain size of the granular filler is 5-200 mm.|6. The method for forming soil by co-weathering gas and phosphate tailings according to claim 1, wherein the operation mode of the biological filter bed is methane oxidizing bacteria liquid intermittent infiltration or methane oxidizing bacteria liquid continuous circulation leaching. (CN119076589)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of waste resource utilization, and particularly relates to a method for forming soil by synergistic weathering of gas and phosphate tailings.|BACKGROUND ART|[0002] In the coal exploitation process, a large amount of gas is discharged, the gas contains a large amount of methane, and the greenhouse effect caused by the methane is 20-30 times that of carbon dioxide with the same mass. The direct discharge of a large amount of gas causes serious carbon emission and resource waste. The phosphate tailings are solid wastes generated after the phosphate ores are beneficiated, are mainly subjected to stacking landfill treatment at present, occupy a large amount of land resources, destroy ecological environment, and waste resources due to the fact that the tailings contain a large amount of phosphate minerals. The prior art is used for treating and recycling the phosphate tailings, because the physical separation method is dependent on gravity, magnetism or floatation and other principles, and can require complex equipment and operation, so that the treatment cost is high, and because the chemical treatment method involves changing the chemical property in the tailings by an extraction-back extraction method, a carbonization method or a calcination-leaching method, harmful substances can be introduced or waste water which is difficult to treat is generated, so that the environmental pollution risk is high. Currently, no method for co-processing and recycling gas and phosphate tailings exists in the prior art.|[0003] For this reason, it is necessary to develop a method for the synergistic weathering of gas and phosphate tailings into soil which can solve the above problems.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a method for forming soil by the synergistic weathering of methane and phosphate tailings, which utilizes organic acid produced by methane biochemical degradation of methane by methane oxidizing bacteria to accelerate decomposition, reconstruction and weathering stabilization of various minerals in the phosphate tailings, promote activation and release of phosphate fertilizer in the phosphate tailings, realize organic matter conversion of methane in weathered products, finally realize rapid weathering of biological carbon fixation of the methane and the phosphate tailings into soil, and realize synergistic treatment and recycling of the methane and the phosphate tailings.|[0005] The object of the invention is achieved in that it comprises the following steps:| S1, preparing phosphate tailings into particle filler, loading methane-oxidizing bacteria on the particle filler, and constructing a biological filter bed which takes phosphate tailings particles as a biological membrane carrier and methane-oxidizing bacteria as dominant microorganisms; | S2, introducing gas into the biological filter bed, wherein the methane concentration in the gas is 0.1-30% by volume, the methane in the gas is biologically oxidized by methane oxidizing bacteria, and methane metabolites (organic acid, extracellular polymers, soluble microorganism products and the like) accelerate mineral decomposition reconstruction of phosphate tailing particles, release effective phosphorus components and obtain weathered products, and the process also realizes proliferation of the methane oxidizing bacteria. |[0006] Methane-oxidizing bacteria (MOB) are microorganisms capable of metabolizing methane as the sole carbon and energy source, and are widely available in the environment to biocatalytically oxidize methane. The biological oxidation process of methane not only can metabolize a large amount of organic acid, but also can be used as a main driving force for biological weathering, and can accelerate the weathering decomposition and reconstruction of silicate minerals, carbonic acid minerals and the like. The growth and proliferation process of methane-oxidizing bacteria can also produce a large amount of organic matters such as Extracellular Polymers (EPS), soluble Microorganism Products (SMP) and the like, so that the organic carbon content of the weathered products can be effectively improved, and the ventilation, soil moisture conservation and fertilizer storage performance of the weathered products of the phosphate tailings can be improved.|[0007] Preferably, the methane-oxidizing bacteria include one or more of methylobacterium (Methylobacter), methylococcus (Methylococcus), methyl monad (Methylomonas), methyl micrococcus (Methylomicrobium), methyl sarcina (Methylosarcina), methyl campylobacter (Methylosinus), methyl cystomycetes (Methylocystis), subtype Ib bacteria (Methylococcus and Methylocaldum).|[0008] Preferably, the phosphate tailings are tailings left after ore dressing and concentrate extraction.|[0009] Preferably, before the step S1 is performed to prepare the particle filler, a binder is added to the phosphate tailings and uniformly mixed, wherein the binder comprises one or more of bentonite, sodium silicate and aluminum dihydrogen phosphate.|[0010] Preferably, the step S1 is carried out to prepare the granular filler, namely, the granular filler is obtained by pressing the phosphate tailings through a granulator or a molding press and then sintering the phosphate tailings, wherein the particle size of the granular filler is 5-200 mm.|[0011] Preferably, the operation mode of the biological filter bed is intermittent infiltration of methane-oxidizing bacteria liquid or continuous circulating leaching of methane-oxidizing bacteria liquid, wherein intermittent infiltration is intermittent infiltration, and the weathering products on the surfaces of the phosphate tailing particles are dissolved and stripped.|[0012] The invention adopts the technical principle that methane in the gas is oxidized and metabolized by methane oxidizing bacteria to be oxidized into organic acid, soluble organic carbon and the like, so that the rapid removal of the gas and biological carbon fixation are realized. The organic acid of the metabolite of methane oxidizing bacteria accelerates the decomposition and reconstruction of minerals in the phosphate tailings, the soluble organic carbon in the metabolite is helpful for the release of the phosphate of the apatite, and the organic fertilizer efficiency of the weathered product of the phosphate tailings is improved to form high-quality soil.|[0013] Compared with the prior art, the invention has the following technical effects:| 1. The invention utilizes methane oxidizing bacteria to carry out biological oxidation on methane in gas, and metabolites are organic acid, extracellular polymer, dissoluble microorganism products and the like, and carry out corrosion and ion exchange effects on silicate minerals, carbonate minerals, phosphorus-containing minerals and the like in the phosphate tailings, thereby promoting the biological weathering of the phosphate tailings. The efflorescence not only accelerates the decomposition reconstruction and stabilization process of the phosphate tailings, but also promotes the release of the available phosphorus, and remarkably improves the proportion of the available phosphorus in the efflorescence product. |[0014] 2. The invention utilizes the adsorption and adhesion effects of the metabolic products of the methane oxidized bacteria biological oxidation methane to effectively improve the organic fertilizer efficiency and the agglomeration of the weathered products of the phosphate tailings. In the process, the organic carbon conversion and biological carbon fixation of methane are realized, and the ventilation, soil moisture conservation and fertilizer storage performances of the weathered products are obviously improved, so that the weathered products can be used as ecological matrix soil, and the resource utilization conversion of the phosphate tailings from large industrial solid wastes to the ecological matrix soil is realized.|[0015] 3. The invention realizes the proliferation of methane-oxidizing bacteria in the process of methane biological oxidation, and the phosphate tailings also play a role of a carrier. Under the adsorption and adhesion effects of the surface of the phosphate tailings, the methane-oxidizing bacteria greatly promote the agglomeration of weathered products, and the process further accelerates the weathering of the phosphate tailings and the proliferation of the methane-oxidizing bacteria to form a synergistic effect.|DRAWINGS DESCRIPTION|[0016] FIG. 1 is a schematic flow chart of the method of the invention.|INVENTION MODE|Detailed Description|[0017] The invention is further described below with reference to examples and drawings, but is not limited in any way, and any changes or substitutions based on the teachings of the invention are intended to fall within the scope of the invention.|[0018] Example 1|As shown in fig. 1, the method for forming soil by the synergistic weathering of the gas and the phosphate tailings in the embodiment comprises the following steps:| S1, adding bentonite into phosphate tailings, uniformly mixing, pressing and sintering the phosphate tailings to prepare particle fillers with the particle size of 10 mm, wherein the phosphate tailings are tailings left after ore dressing and concentrate extraction, and loading methane-oxidizing bacteria on the particle fillers to construct a biological filter bed with phosphate tailings particles as a biological film carrier and methane-oxidizing bacteria as dominant microorganisms, wherein the methane-oxidizing bacteria are mixed flora of methylcyst bacteria (Methylocystis) and subtype Ib bacteria (Methylococcus and Methylocaldum); | s2, introducing gas into the biological filter bed, wherein the concentration of methane in the gas is 8% by volume, the methane in the gas is biologically oxidized by methane-oxidizing bacteria, the methane metabolite accelerates the mineral decomposition and reconstruction of the phosphate tailing particles, and the effective phosphorus component is released, so that a weathered product is obtained, and the weathered product is sent out to serve as ecological matrix soil, wherein methane-oxidizing bacteria liquid is intermittently infiltrated. |[0019] Example 2|In the method for forming soil by synergistic weathering of gas and phosphate tailings in the embodiment, methane-oxidizing bacteria are mixed bacteria of methyl bacillus (Methylobacter), methyl coccus (Methylococcus) and methyl monad (Methylomonas), particle filler particle size is 20mm, bentonite is replaced by sodium silicate, methane concentration in the gas is 10% by volume, and the rest is the same as in the embodiment 1.|[0020] Example 3|In the method for forming soil by synergistic weathering of gas and phosphate tailings, methane-oxidizing bacteria are methyl bacillus (Methylobacter), the methane concentration in the gas is 0.1% by volume, methane-oxidizing bacteria liquid is continuously and circularly leached, and the rest is the same as in example 1.|[0021] Example 4|In the method for forming soil by synergistic weathering of gas and phosphate tailings, methane-oxidizing bacteria are methyl cocci (Methylococcus), the methane concentration in the gas is 30% by volume, methane-oxidizing bacteria liquid is continuously and circularly leached, and the rest is the same as in example 1.|[0022] Example 5|In the method for forming soil by synergistic weathering of gas and phosphate tailings, methane-oxidizing bacteria are methyl monad (Methylomonas), the methane concentration in the gas is 15% by volume, methane-oxidizing bacteria liquid is continuously and circularly leached, and the rest is the same as in example 1.|[0023] Example 6|The method for forming soil by co-weathering gas and phosphate tailings in this example except that methane-oxidizing bacteria are methyl microorganisms (Methylomicrobium) is the same as in example 1.|[0024] Example 7|In this example, the method for forming soil by co-weathering gas and phosphate tailings was the same as in example 1 except that methane-oxidizing bacteria were methyl sarcina (Methylosarcina).|[0025] Example 8|In this example, methane-oxidizing bacteria were removed as Methylotrichum (Methylosinus) by a method of forming soil by co-weathering with phosphate tailings, and the rest was the same as in example 1.|[0026] Example 9|In this example, methane-oxidizing bacteria were removed as methylcyst bacteria (Methylocystis) by a method for forming soil by co-weathering with phosphate tailings, and the rest was the same as in example 1.|[0027] Example 10|The method for forming soil by co-weathering gas and phosphate tailings in this example except that methane-oxidizing bacteria were subtype Ib bacteria (Methylococcus and Methylocaldum) was used, the rest was the same as in example 1.|[0028] Example 11|In this example, methane-oxidizing bacteria were mixed populations of methylobacterium (Methylobacter), methylococcus (Methylococcus), methylomonas (Methylomonas), methylobacterium (Methylomicrobium), methylosarcina (Methylosarcina), methylocampylobacter (Methylosinus), methylocyst (Methylocystis) and subtype Ib bacteria (Methylococcus and Methylocaldum), and the rest were the same as in example 1. (CN119076589)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of waste resource utilization, and particularly relates to a method for forming soil by synergistic weathering of gas and phosphate tailings.|BACKGROUND ART|[0002] In the coal exploitation process, a large amount of gas is discharged, the gas contains a large amount of methane, and the greenhouse effect caused by the methane is 20-30 times that of carbon dioxide with the same mass. The direct discharge of a large amount of gas causes serious carbon emission and resource waste. The phosphate tailings are solid wastes generated after the phosphate ores are beneficiated, are mainly subjected to stacking landfill treatment at present, occupy a large amount of land resources, destroy ecological environment, and waste resources due to the fact that the tailings contain a large amount of phosphate minerals. The prior art is used for treating and recycling the phosphate tailings, because the physical separation method is dependent on gravity, magnetism or floatation and other principles, and can require complex equipment and operation, so that the treatment cost is high, and because the chemical treatment method involves changing the chemical property in the tailings by an extraction-back extraction method, a carbonization method or a calcination-leaching method, harmful substances can be introduced or waste water which is difficult to treat is generated, so that the environmental pollution risk is high. Currently, no method for co-processing and recycling gas and phosphate tailings exists in the prior art.|[0003] For this reason, it is necessary to develop a method for the synergistic weathering of gas and phosphate tailings into soil which can solve the above problems.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a method for forming soil by the synergistic weathering of methane and phosphate tailings, which utilizes organic acid produced by methane biochemical degradation of methane by methane oxidizing bacteria to accelerate decomposition, reconstruction and weathering stabilization of various minerals in the phosphate tailings, promote activation and release of phosphate fertilizer in the phosphate tailings, realize organic matter conversion of methane in weathered products, finally realize rapid weathering of biological carbon fixation of the methane and the phosphate tailings into soil, and realize synergistic treatment and recycling of the methane and the phosphate tailings.|[0005] The object of the invention is achieved in that it comprises the following steps:| S1, preparing phosphate tailings into particle filler, loading methane-oxidizing bacteria on the particle filler, and constructing a biological filter bed which takes phosphate tailings particles as a biological membrane carrier and methane-oxidizing bacteria as dominant microorganisms; | S2, introducing gas into the biological filter bed, wherein the methane concentration in the gas is 0.1-30% by volume, the methane in the gas is biologically oxidized by methane oxidizing bacteria, and methane metabolites (organic acid, extracellular polymers, soluble microorganism products and the like) accelerate mineral decomposition reconstruction of phosphate tailing particles, release effective phosphorus components and obtain weathered products, and the process also realizes proliferation of the methane oxidizing bacteria. |[0006] Methane-oxidizing bacteria (MOB) are microorganisms capable of metabolizing methane as the sole carbon and energy source, and are widely available in the environment to biocatalytically oxidize methane. The biological oxidation process of methane not only can metabolize a large amount of organic acid, but also can be used as a main driving force for biological weathering, and can accelerate the weathering decomposition and reconstruction of silicate minerals, carbonic acid minerals and the like. The growth and proliferation process of methane-oxidizing bacteria can also produce a large amount of organic matters such as Extracellular Polymers (EPS), soluble Microorganism Products (SMP) and the like, so that the organic carbon content of the weathered products can be effectively improved, and the ventilation, soil moisture conservation and fertilizer storage performance of the weathered products of the phosphate tailings can be improved.|[0007] Preferably, the methane-oxidizing bacteria include one or more of methylobacterium (Methylobacter), methylococcus (Methylococcus), methyl monad (Methylomonas), methyl micrococcus (Methylomicrobium), methyl sarcina (Methylosarcina), methyl campylobacter (Methylosinus), methyl cystomycetes (Methylocystis), subtype Ib bacteria (Methylococcus and Methylocaldum).|[0008] Preferably, the phosphate tailings are tailings left after ore dressing and concentrate extraction.|[0009] Preferably, before the step S1 is performed to prepare the particle filler, a binder is added to the phosphate tailings and uniformly mixed, wherein the binder comprises one or more of bentonite, sodium silicate and aluminum dihydrogen phosphate.|[0010] Preferably, the step S1 is carried out to prepare the granular filler, namely, the granular filler is obtained by pressing the phosphate tailings through a granulator or a molding press and then sintering the phosphate tailings, wherein the particle size of the granular filler is 5-200 mm.|[0011] Preferably, the operation mode of the biological filter bed is intermittent infiltration of methane-oxidizing bacteria liquid or continuous circulating leaching of methane-oxidizing bacteria liquid, wherein intermittent infiltration is intermittent infiltration, and the weathering products on the surfaces of the phosphate tailing particles are dissolved and stripped.|[0012] The invention adopts the technical principle that methane in the gas is oxidized and metabolized by methane oxidizing bacteria to be oxidized into organic acid, soluble organic carbon and the like, so that the rapid removal of the gas and biological carbon fixation are realized. The organic acid of the metabolite of methane oxidizing bacteria accelerates the decomposition and reconstruction of minerals in the phosphate tailings, the soluble organic carbon in the metabolite is helpful for the release of the phosphate of the apatite, and the organic fertilizer efficiency of the weathered product of the phosphate tailings is improved to form high-quality soil.|[0013] Compared with the prior art, the invention has the following technical effects:| 1. The invention utilizes methane oxidizing bacteria to carry out biological oxidation on methane in gas, and metabolites are organic acid, extracellular polymer, dissoluble microorganism products and the like, and carry out corrosion and ion exchange effects on silicate minerals, carbonate minerals, phosphorus-containing minerals and the like in the phosphate tailings, thereby promoting the biological weathering of the phosphate tailings. The efflorescence not only accelerates the decomposition reconstruction and stabilization process of the phosphate tailings, but also promotes the release of the available phosphorus, and remarkably improves the proportion of the available phosphorus in the efflorescence product. |[0014] 2. The invention utilizes the adsorption and adhesion effects of the metabolic products of the methane oxidized bacteria biological oxidation methane to effectively improve the organic fertilizer efficiency and the agglomeration of the weathered products of the phosphate tailings. In the process, the organic carbon conversion and biological carbon fixation of methane are realized, and the ventilation, soil moisture conservation and fertilizer storage performances of the weathered products are obviously improved, so that the weathered products can be used as ecological matrix soil, and the resource utilization conversion of the phosphate tailings from large industrial solid wastes to the ecological matrix soil is realized.|[0015] 3. The invention realizes the proliferation of methane-oxidizing bacteria in the process of methane biological oxidation, and the phosphate tailings also play a role of a carrier. Under the adsorption and adhesion effects of the surface of the phosphate tailings, the methane-oxidizing bacteria greatly promote the agglomeration of weathered products, and the process further accelerates the weathering of the phosphate tailings and the proliferation of the methane-oxidizing bacteria to form a synergistic effect.|DRAWINGS DESCRIPTION|[0016] FIG. 1 is a schematic flow chart of the method of the invention.|INVENTION MODE|Detailed Description|[0017] The invention is further described below with reference to examples and drawings, but is not limited in any way, and any changes or substitutions based on the teachings of the invention are intended to fall within the scope of the invention.|[0018] Example 1|As shown in fig. 1, the method for forming soil by the synergistic weathering of the gas and the phosphate tailings in the embodiment comprises the following steps:| S1, adding bentonite into phosphate tailings, uniformly mixing, pressing and sintering the phosphate tailings to prepare particle fillers with the particle size of 10 mm, wherein the phosphate tailings are tailings left after ore dressing and concentrate extraction, and loading methane-oxidizing bacteria on the particle fillers to construct a biological filter bed with phosphate tailings particles as a biological film carrier and methane-oxidizing bacteria as dominant microorganisms, wherein the methane-oxidizing bacteria are mixed flora of methylcyst bacteria (Methylocystis) and subtype Ib bacteria (Methylococcus and Methylocaldum); | s2, introducing gas into the biological filter bed, wherein the concentration of methane in the gas is 8% by volume, the methane in the gas is biologically oxidized by methane-oxidizing bacteria, the methane metabolite accelerates the mineral decomposition and reconstruction of the phosphate tailing particles, and the effective phosphorus component is released, so that a weathered product is obtained, and the weathered product is sent out to serve as ecological matrix soil, wherein methane-oxidizing bacteria liquid is intermittently infiltrated. |[0019] Example 2|In the method for forming soil by synergistic weathering of gas and phosphate tailings in the embodiment, methane-oxidizing bacteria are mixed bacteria of methyl bacillus (Methylobacter), methyl coccus (Methylococcus) and methyl monad (Methylomonas), particle filler particle size is 20mm, bentonite is replaced by sodium silicate, methane concentration in the gas is 10% by volume, and the rest is the same as in the embodiment 1.|[0020] Example 3|In the method for forming soil by synergistic weathering of gas and phosphate tailings, methane-oxidizing bacteria are methyl bacillus (Methylobacter), the methane concentration in the gas is 0.1% by volume, methane-oxidizing bacteria liquid is continuously and circularly leached, and the rest is the same as in example 1.|[0021] Example 4|In the method for forming soil by synergistic weathering of gas and phosphate tailings, methane-oxidizing bacteria are methyl cocci (Methylococcus), the methane concentration in the gas is 30% by volume, methane-oxidizing bacteria liquid is continuously and circularly leached, and the rest is the same as in example 1.|[0022] Example 5|In the method for forming soil by synergistic weathering of gas and phosphate tailings, methane-oxidizing bacteria are methyl monad (Methylomonas), the methane concentration in the gas is 15% by volume, methane-oxidizing bacteria liquid is continuously and circularly leached, and the rest is the same as in example 1.|[0023] Example 6|The method for forming soil by co-weathering gas and phosphate tailings in this example except that methane-oxidizing bacteria are methyl microorganisms (Methylomicrobium) is the same as in example 1.|[0024] Example 7|In this example, the method for forming soil by co-weathering gas and phosphate tailings was the same as in example 1 except that methane-oxidizing bacteria were methyl sarcina (Methylosarcina).|[0025] Example 8|In this example, methane-oxidizing bacteria were removed as Methylotrichum (Methylosinus) by a method of forming soil by co-weathering with phosphate tailings, and the rest was the same as in example 1.|[0026] Example 9|In this example, methane-oxidizing bacteria were removed as methylcyst bacteria (Methylocystis) by a method for forming soil by co-weathering with phosphate tailings, and the rest was the same as in example 1.|[0027] Example 10|The method for forming soil by co-weathering gas and phosphate tailings in this example except that methane-oxidizing bacteria were subtype Ib bacteria (Methylococcus and Methylocaldum) was used, the rest was the same as in example 1.|[0028] Example 11|In this example, methane-oxidizing bacteria were mixed populations of methylobacterium (Methylobacter), methylococcus (Methylococcus), methylomonas (Methylomonas), methylobacterium (Methylomicrobium), methylosarcina (Methylosarcina), methylocampylobacter (Methylosinus), methylocyst (Methylocystis) and subtype Ib bacteria (Methylococcus and Methylocaldum), and the rest were the same as in example 1. Family Number|(112511768)|112511768|Abstract|(CN119076589 A)|The invention discloses a method for synergistically weathering gas and phosphate tailings into soil . The method comprises the following steps : firstly , preparing phosphate tailings into granular filler , loading methane - oxidizing bacteria on the granular filler , and constructing a biological filter bed which takes phosphate tailings particles as a biofilm carrier and takes the methane - oxidizing bacteria as dominant microorganisms ; gas is introduced into the biological filter bed , the concentration of methane in the gas is 0.1%-30% by volume , methane in the gas is biologically oxidized by methane - oxidizing bacteria , mineral decomposition and reconstruction of phosphate tailing particles are accelerated by methane metabolites , available phosphorus components are released , and weathered products are obtained . According to the method , organic acid produced by biochemical degradation of methane through methane - oxidizing bacteria is utilized , decomposition reconstruction and weathering stabilization of various minerals in the phosphate tailings are accelerated , activation and release of phosphate fertilizer in the phosphate tailings are promoted , organic matter conversion of methane in weathered products is achieved , finally , biological carbon sequestration of methane and the phosphate tailings are rapidly weathered into soil , and the phosphorus tailings are rapidly decomposed into soil . Co - processing and recycling of the gas and the phosphate tailings are realized . |CPC codes|(CN119076589 A)|A01B - 079/00 |A01B - 079/02 |IPC codes|(CN119076589 A)|A01B - 079/00 |A01B - 079/02 |Title|(CN119076589 A)|Method for cooperatively weathering gas and phosphate tailings into soil | Environmental technology|Other special machines A01B-079/00|A01B-079/02|B09B-003/25|B09B-003/60|B09B-003/70|B09B-2101/55|Y02A-050/20 A01B-079/00|A01B-079/02|B09B-003/25|B09B-003/60|B09B-003/70|B09B-2101/55|Y02A-050/20 A01B-079/00|A01B-079/02|B09B-003/25|B09B-003/60|B09B-003/70|B09B-101/55 A01B-079/00|A01B-079/02|B09B-003/25|B09B-003/60|B09B-003/70|B09B-101/55 PENDING (CN119076589)|PENDING ALIVE (CN119076589)|ALIVE (CN119076589)|LEGAL DETAILS FOR CN119076589|Actual or expected expiration date=2044-08-14|Legal state=ALIVE|Status=PENDING|Event publication date=2024-08-14|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202411116320|Application date=2024-08-14|Standardized application number=2024CN-1116320|Event publication date=2024-12-06|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119076589|Publication stage code=A|Publication date=2024-12-06|Standardized publication number=CN119076589|Event publication date=2024-12-06|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-12-24|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN119076589)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRdNo+GlOYZfFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000075512299&ekey=2143&xpn=CN119076589&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=WPhvToGRZyx0TYcyM78bJpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN119076589)|CN (CN119076589)|NAME=KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN119076589)|NAME=ZHANG YANG;Kunming Tongju Patent Agency Co., Ltd. , REG=53214NAME=ZHANG YU;Kunming Tongju Patent Agency Co., Ltd. , REG=53214 (CN119076589)|NAME=HU XUEWEI|NAME=YANG YANG|NAME=SONG HAORAN|NAME=ZHAO QUN|NAME=TIAN SENLIN|NAME=ZHANG QING 0 1 Titre: (CN119076589)|Method for cooperatively weathering gas and phosphate tailings into soil Résumé: (CN119076589)|The invention discloses a method for synergistically weathering gas and phosphate tailings into soil. The method comprises the following steps: firstly, preparing phosphate tailings into granular filler, loading methane-oxidizing bacteria on the granular filler, and constructing a biological filter bed which takes phosphate tailings particles as a biofilm carrier and takes the methane-oxidizing bacteria as dominant microorganisms; gas is introduced into the biological filter bed, the concentration of methane in the gas is 0.1%-30% by volume, methane in the gas is biologically oxidized by methane-oxidizing bacteria, mineral decomposition and reconstruction of phosphate tailing particles are accelerated by methane metabolites, available phosphorus components are released, and weathered products are obtained. According to the method, organic acid produced by biochemical degradation of methane through methane-oxidizing bacteria is utilized, decomposition reconstruction and weathering stabilization of various minerals in the phosphate tailings are accelerated, activation and release of phosphate fertilizer in the phosphate tailings are promoted, organic matter conversion of methane in weathered products is achieved, finally, biological carbon sequestration of methane and the phosphate tailings are rapidly weathered into soil, and the phosphorus tailings are rapidly decomposed into soil. Co-processing and recycling of the gas and the phosphate tailings are realized. 66 Abstract gpt-4o-mini uncertain The method involves weathering phosphate tailings and mentions biological carbon sequestration, but it primarily focuses on methane oxidation and phosphorus release rather than explicit CO₂ capture or mineral carbonation.
67 CN202310772521 CN202310772521 CN116854421 106780457 CN116854421 A 2023-10-10 [CN116854421] 2023-06-27 2023-06-27 2023-10-10 (CN116854421)|2043-06-27 (CN116854421)|Method for preparing polyphenyl granule concrete by utilizing carbonized recycled fine aggregate and uniformity testing method (CN116854421)|The invention discloses a method for preparing polyphenyl granule concrete by utilizing carbonized recycled fine aggregate, which comprises the following steps: firstly, crushing waste concrete blocks to obtain recycled fine aggregate; then putting the recycled fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; cO2 is introduced into the carbonization furnace until the pressure intensity is 0.1-0.4 MPa, carbonization is performed for 12-48 h, and carbonized fine aggregate is obtained; and finally, uniformly mixing the cement, the river sand, the carbonized fine aggregate and the EPS particles according to a mass ratio of 600: 240-360: 120-240: 7.5, adding water according to a water-cement ratio of 0.46, and uniformly mixing. The method has the remarkable effects that the performance of the recycled aggregate is improved by performing carbonization pretreatment on the recycled fine aggregate prepared from the waste concrete, a reference basis is provided for subsequent engineering application of the recycled fine aggregate subjected to carbonization pretreatment, a large amount of waste concrete and polystyrene resources can be effectively recycled, natural gravel resources are saved, and the economic benefit is increased. Environment protection is facilitated, building solid waste is reasonably utilized and subjected to carbon sequestration, and the new direction of green, low-carbon and energy-saving building development is met. CHONGQING HEFENG ZHUJIAN TECHNOLOGY (CN116854421)|CHONGQING HEFENG ZHUJIAN TECHNOLOGY CO., LTD. ([CN]) SU XIN|FENG CHUNLAN|YOU YARAN|FENG RENJIANG|OUYANG YUHUI|BU CHANGMING|ZHANG MINGTAO|SUN YI|SHI YANGXI|ZHANG XUETAO|TANG JING (CN116854421)|SU XIN|FENG CHUNLAN|YOU YARAN|FENG RENJIANG|OUYANG YUHUI|BU CHANGMING|ZHANG MINGTAO|SUN YI|SHI YANGXI|ZHANG XUETAO|TANG JING (CN116854421)|YAO KUN;CHONGQING QIANSHI PATENT AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 50259 (CN116854421)|Comparing the recycled fine aggregate concrete which is not carbonized and pretreated in the same period with the recycled fine aggregate concrete which is carbonized and treated under different conditions, the method has the following advantages that: the concrete pretreated by C4T24 carbonization has the improvement effect of 0.38-2.68%, 2.74-5.88% and 5.33-7.49% of compressive strength respectively at 3d, 7d and 28d, and the maximum compressive strength value is 9.61MPa.| (CN116854421)|1. A method for preparing polyphenyl granule concrete by using carbonized regenerated fine aggregate is characterized by comprising the following steps: Step one, preparing recycled fine aggregate;crushing the waste concrete blocks to obtain recycled fine aggregate;firstly, stripping steel bars from waste concrete to obtain waste concrete blocks, primarily crushing to obtain 25-50mm recycled coarse aggregate, crushing by a jaw crusher, and screening by a vibrating screen to obtain recycled fine aggregate;step two, putting the regenerated fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; CO is introduced again 2 The pressure in the carbonization furnace is 0.1-0.4MPa, and carbonization is carried out for 12-48 hours to obtain carbonized fine aggregate;step three, 600:240-360:120-240: and mixing cement, river sand, carbonized fine aggregate and EPS particles uniformly in a mass ratio of 7.5, and adding water according to a water-cement ratio of 0.46, and mixing uniformly.| (CN116854421)|The invention discloses a method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate, which comprises the steps of firstly crushing waste concrete blocks to obtain the recycled fine aggregate; putting the recycled fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; CO is introduced again 2 The pressure in the carbonization furnace is 0.1-0.4MPa, and carbonization is carried out for 12-48 hours to obtain carbonized fine aggregate; finally, 600:240-360:120-240: and mixing cement, river sand, carbonized fine aggregate and EPS particles uniformly in a mass ratio of 7.5, and adding water according to a water-cement ratio of 0.46, and mixing uniformly.|The invention relates to the field of building materials, in particular to recycling of building waste.|This also explains from another aspect that the carbonization effect is affected by the carbonization time so that the carbonization effect does not show an increasing trend with time to some extent, the improvement effect thereof is affected by the improvement of early carbonization, so that the later carbonization time increases but the subsequent carbon dioxide cannot sufficiently enter the inside of the recycled aggregate to provide the carbonization reaction raw material so that the improvement effect gradually declines.| (CN116854421)|RECYCLED FINE AGGREGATE(100,92)|POLYPHENYL GRANULE(100,16)|FINE AGGREGATE(100,10)|CARBONIZED REGENERATED FINE AGGREGATE(100,7)|UNIFORMITY TESTING(100,1)|CARBONIZATION FURNACE(75,15)|CARBON FINE AGGREGATE(54,4)|CARBONIZED FINE AGGREGATE(51,5)|RIVER SAND(35,5)|EPS PARTICLE(33,6)|EARLY CARBONIZATION(31,1)|RECYCLED AGGREGATE(30,25)|CARBONIZING PRETREATMENT(30,2)|CARBONIZATION(29,31)|REGENERATED FINE AGGREGATE(29,17)|RECYCLED FINE AGGREGATE CONCRETE(29,10)|CEMENT MIX(29,4)|CARBONIZATION PRETREATMENT(27,24)|PIPE ORIFICE BLOCKING COVER(27,8)|RECYCLED COARSE AGGREGATE(26,2)|VIBRATING SCREEN(23,2)|WASTE CONCRETE BLOCK(22,5)|EMPTYING PIPE(22,4)|FINE AGGREGATE CONCRETE(20,13)|POLYSTYRENE RESOURCE(20,2)|STONE RESOURCE(20,2)|RECYCLEDTHE(19,1)|CARBONIZATION TREATMENT(18,18)|CYLINDRICAL SAMPLE(18,8)|TANK COVER(17,4)|TREND(17,1)|POLYPHENYL PARTICLE INFORMATION PARAMETER(16,2)|SUPPORT DISC(15,8)|INTERNAL POLYPHENYL PARTICLE(15,2)|AIR INLET PIPE(14,12)|SEGMENTATION TREATMENT(14,2)|STRIPPING STEEL BAR(14,2)|DECLINE(14,1)|JAW CRUSHER(13,3)|NATURAL SAND(13,2)|CONCRETE(12,32)|BINARY CONVERSION(12,2)|CARBON SEALING(12,1)|ENERGY SAVING BUILDING(12,1)|BUILDING WASTE(11,1)|LATE CARBONIZATION TIME(11,1)|COMPRESSIVE STRENGTH(10,17)|DECREASING TREND(10,9)|WATER CEMENT RATIO(10,5)|SOFTWARE ANALYSIS(10,2)|SUPPORTING TRAY COMPONENT(10,2)|C4T(9,16)|ANALYSIS IMAGE(9,4)|SUPPORT BLOCK(9,3)|IMAGE ACQUISITION(9,2)|SUPPORT TRAY(9,2)|THERMOMETER(9,2)|DISCHARGING(9,1)|GREEN DEVELOPMENT DIRECTION(9,1)|CARBONIZATION REACTION PRODUCT(8,9)|DRAIN PIPE(8,5)|CARBONIZATION REACTION RAW MATERIAL(8,1)|CARBONIZED AGGREGATE MICROTOPOGRAPHY(8,1)|COMPRESSIVE STRENGTH VALUE(8,1)|FLANGE PLATE(8,1)|POLYPHENYL GRANULE CONCRETE PARAMETER(8,1)|STANDING(8,1)|SPLITTING TENSILE STRENGTH(7,8)|CARBONATION REACTION(7,5)|HUMIDITY(7,4)|MASS RATIO(7,4)|BUILDING SOLID WASTE(7,3)|DIFFRACTION PEAK INTENSITY(7,3)|NOTCH(7,2)|NONCARBONIZED REGENERATED FINE AGGREGATE(7,1)|UNCARBONIZED CEMENT MORTAR(7,1)|CARBONIZED AGGREGATE DIFFRACTION PATTERN(6,2)|INDOOR ENVIRONMENT(6,2)|MICROSCOPIC MORPHOLOGY(6,2)|POLYPHENYL PARTICLE DISTRIBUTION(6,2)|REGENERATION FINE AGGREGATE(6,2)|RGB(6,2)|AGGREGATE POLYPHENYL PARTICLE CONCRETE(6,1)|CARBON CEMENT SLURRY(6,1)|CARBONIZED RECYCLED FINE AGGREGATE(6,1)|POLYPHENYL GRANULAR CONCRETE(6,1)|POLYPHENYL GRANULE UNIFORMITY TEST(6,1)|RAW AGGREGATE MORTAR(6,1)|RECYCLED FINE AGGREGATE MORTAR(6,1)|RECYCLED FINE AGGREGATE POLYPHENYL(6,1)|UNTREATED RECYCLED AGGREGATE(6,1)|CARBONIZATION TIME(5,31)|INTERFACE TRANSITION ZONE(5,6)|CUT IMAGE(5,2)|GELLED SUBSTANCE(5,2)|NEGATIVE PRESSURE SUCTION PIPE(5,2)|NOISE REDUCTION TREATMENT(5,2)|TAMPING TRENCH(5,2)|UNIFORMLY STIRRING NATURAL AGGREGATE(5,2)|CARBONIZATION TIMETHE(5,1)|CARBONIZED FINE AGGREGATE PH(5,1)|NATURAL RIVER SAND AGGREGATE(5,1)|POLYSTYRENE PARTICLE WALLBOARD(5,1)|RECYCLED FINE AGGREGATE BATCH(5,1)|CARBON DIOXIDE(4,9)|CONCRETE DRY DENSITY(4,3)|FINE AGGREGATE SUBSTITUTION RATE(4,3)|CONCAVE SURFACE(4,2)|DEMOULDING TREATMENT(4,2)|DRAIN VALVE(4,2)|INFRARED BLAST(4,2)|PUTTING CEMENT(4,2)|SAFETY VALVE(4,2)|SEWAGE UPPER END(4,2)|SMALL HOLE(4,2)|UPPER PIPE WALL(4,2)|ACCELERATING CARBONIZATION(4,1)|AGGREGATE POLYSTYRENE(4,1)|AGGREGATE SATURATION(4,1)|BUILDING MATERIAL(4,1)|CARBONIZABLE SUBSTANCE(4,1)|CARBONIZATION INFLUENCE(4,1)|CARBONIZATION PARAMETER(4,1)|CARBONIZATION PRETREATMENT GROUP(4,1)|CARBONIZATION REACTION INHIBITION(4,1)|CEMENT PASTE BONDING CAPABILITY(4,1)|CIVIL BUILDING(4,1)|CONCRETE CUBE(4,1)|CONCRETE DECREASE FLUIDITY(4,1)|CRUSHED AGGREGATE(4,1)|CRUSHING TRENCH(4,1)|DISCARDED CONCRETE(4,1)|EARLY CARBONIZATION GAIN(4,1)|EARLY CARBONIZATION REACTION(4,1)|FINE AGGREGATE CARBONIZED AGGREGATE(4,1)|GRANULE CONCRETE DECREASE(4,1)|IRREGULAR MORPHOLOGY(4,1)|POLYPHENYL PARTICLE PARAMETER(4,1)|POLYSTYRENE PARTICLE RECYCLED FINE(4,1)|PROFOUND SIGNIFICANCE(4,1)|RECYCLED CONCRETE FINE AGGREGATE(4,1)|RECYCLED MORTAR(4,1)|REGENERATE FINE AGGREGATE(4,1)|REGENERATED AGGREGATE WHOLE(4,1)|REGENERATED COARSE AGGREGATE(4,1)|SAND GRADING(4,1)|SUSTAINABLE UTILIZATION(4,1)|UNCARBONATED SLURRY(4,1)|UNIFORMITY QUANTIZATION(4,1)|WASTE MORTAR(4,1)|XRD DIFFRACTOMETER(4,1)|INNER WALL(3,6)|SPLIT TENSILE STRENGTH(3,3)|STANDARD CURING(3,3)|HYDRATION PRODUCT(3,2)|MICRO POWDER RECYCLING(3,2)|MINIMUM CRUSHING(3,2)|POSITION DISTRIBUTION(3,2)|PRESSURE GAUGE(3,2)|REGENERATED MICRO POWDER(3,2)|XRD DIFFRACTION PATTERN(3,2)|ADHESIVE MORTAR(3,1)|AGGREGATE CHANGE PORE(3,1)|AGGREGATE CRUSHING INDEX(3,1)|AGGREGATE GAP(3,1)|CALCIUM ALUMINATE HYDRATE(3,1)|CALCIUM CARBONATE CRYSTAL DECOMPOSITION(3,1)|CALCIUM CARBONATE DIFFRACTION PEAK(3,1)|CEMENT MORTAR COMPONENT(3,1)|DRY CONCRETE DENSITY PLOT(3,1)|EXPANDED POLYSTYRENE(3,1)|GROWTH TREND(3,1)|PARTICLE FINE RECYCLING(3,1)|PARTICLE QUANTITY UNIFORMITY(3,1)|PROBABLY CAUSED BYUNDER(3,1)|RAW MORTAR(3,1)|RECYCLED AGGREGATE PHYSICAL PROPERTY(3,1)|RECYCLED CONCRETE COARSE AGGREGATE(3,1)|RECYCLED MICRO POWDER EXISTENCE(3,1)|SLUMP DECREASE(3,1)|UNIFORMITY DISTRIBUTION SITUATION(3,1)|WATER AGGREGATION PHENOMENON(3,1)|ARC SHAPED SURFACE(2,6)|SEWAGE DRAIN(2,4)|CARBON DIOXIDE GAS(2,3)|MAXIMUM STRENGTH(2,3)|QUALITY LOSS(2,3)|STEP THREE(2,3)|C4T24R(2,2)|CALCITE(2,2)|CARBONIZATION GROUP(2,2)|CARBONIZATION PRESSURE CONDITION(2,2)|DRYING TREATMENT(2,2)|LOOSE BULK DENSITY(2,2)|MUD BLOCK(2,2)|RECYCLED AGGREGATE PERFORMANCE(2,2)|STEEL TEST DIE(2,2)|ADDITIVE(2,1)|AGGLOMERATION(2,1)|AGGREGATE BULK DENSITY(2,1)|ANNUAL GROWTH SPEED(2,1)|BROKEN ROCK(2,1)|BUILDING ASSEMBLY(2,1)|CALCIUM CARBONATE DECOMPOSITION(2,1)|CALCIUM HYDROXIDE CONSUMPTION(2,1)|CARBONIZATION CONDITION COMPRESSIVE STRENGTH(2,1)|CARBONIZATION MECHANISM ANALYSIS(2,1)|CARBONIZATION PRESSURE INFLUENCE(2,1)|CARBONIZED PRODUCT(2,1)|CONCRETE REDUCTION(2,1)|CONSTRUCTION PROMOTION(2,1)|DENSE FILM(2,1)|DTG CURVE(2,1)|FINE AGGREGATE CONCRETE NATURE(2,1)|HYDROXIDE ION(2,1)|INCAPABILITY(2,1)|INDUSTRIALIZATION(2,1)|NET BAG(2,1)|RECYCLED CONCRETE DEVELOPMENT(2,1)|STRENGTHENING(2,1)|TESTING UNIFORMITY(2,1)|TIMELY DISSOLVING CARBON DIOXIDE(2,1)|TOTAL RECYCLED AGGREGATE(2,1)| (CN116854421)|1. A method for preparing polyphenyl granule concrete by using carbonized regenerated fine aggregate is characterized by comprising the following steps: |Step one, preparing recycled fine aggregate;|crushing the waste concrete blocks to obtain recycled fine aggregate;|firstly, stripping steel bars from waste concrete to obtain waste concrete blocks, primarily crushing to obtain 25-50mm recycled coarse aggregate, crushing by a jaw crusher, and screening by a vibrating screen to obtain recycled fine aggregate;|step two, putting the regenerated fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; CO is introduced again 2 The pressure in the carbonization furnace is 0.1-0.4MPa, and carbonization is carried out for 12-48 hours to obtain carbonized fine aggregate;|step three, 600:240-360:120-240: and mixing cement, river sand, carbonized fine aggregate and EPS particles uniformly in a mass ratio of 7.5, and adding water according to a water-cement ratio of 0.46, and mixing uniformly.|2. The method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate as set forth in claim 1, wherein: in the second step, the recycled fine aggregate is firstly placed in an indoor environment with the temperature of 22-28 ℃ and the humidity of 45-55%RH for standing for 7d, and then is put into a carbonization furnace for carbonization treatment.|3. The method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate as set forth in claim 1, wherein: in the second step, CO is introduced into the carbonization furnace 2 Until the pressure is 0.4MPa, the carbonization time is 48h.|4. The method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate as set forth in claim 1, wherein: the carbonization furnace comprises a tank body (1) and a tank cover (2) which is buckled on the tank body (1) in a sealing way, wherein a drain pipe (11) and CO are connected to the bottom of the tank body (1) 2 An air inlet pipe (12), wherein a negative pressure suction pipe (13) is connected to the upper part of the tank body (1);|the tank cover (2) is provided with a thermometer (21), a safety valve (22) and an emptying pipe (23).|5. The method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate as set forth in claim 4, wherein: a plurality of supporting tray components are vertically distributed in the tank body (1);|the support tray assembly comprises at least three support blocks (31) and one support disc (32), wherein the support blocks (31) are fixed on the inner wall of the tank body (1), the support discs (32) are tiled in the tank body (1), edges of the support discs (32) are lapped on the corresponding support blocks (31), and yielding notches are formed in the edges of the support discs (32) and correspond to the support blocks (31) one by one.|6. The method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate as set forth in claim 1, wherein: the CO 2 The air inlet pipe (12) is vertically arranged, and the CO 2 The upper part of the air inlet pipe (12) stretches into the tank body (1), and the CO 2 The upper end port of the air inlet pipe (12) is closed, and the CO is formed by 2 The upper pipe wall of the air inlet pipe (12) is provided with a lateral air inlet.|7. The method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate as set forth in claim 1, wherein: the bottom of the inner wall of the tank body (1) is an arc-shaped surface, and the concave surface of the arc-shaped surface faces upwards;|the sewage draining pipe (11) is vertically arranged, the upper end of the sewage draining pipe (11) is connected with the lowest part of the arc-shaped surface, and the pipe orifice at the upper end of the sewage draining pipe (11) is communicated with the tank body (1);|the upper end of the tank body (1) corresponding to the sewage draining pipe (11) is further provided with a pipe orifice blocking cover (14), the pipe orifice blocking cover (14) is buckled at the bottom of the tank body (1), the edge of the pipe orifice blocking cover (14) is fixedly connected with the inner wall of the tank body (1), and the pipe orifice blocking cover (14) is provided with a plurality of small holes.|8. The method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate as set forth in claim 1, wherein: the tank body (1) and the tank cover (2) are respectively provided with flange plates which are matched with each other.|9. The method for preparing polyphenyl granule concrete by using carbonized recycled fine aggregate as set forth in claim 1, wherein: a drain valve is arranged on the drain pipe (11) and is used for discharging CO 2 A pressure reducing valve is arranged on the air inlet pipe (12), and a pressure gauge is arranged on the emptying pipe (23);|at least three supporting legs (4) are arranged outside the tank body (1).|10. A uniformity testing method of polyphenyl granule concrete is characterized by comprising the following steps:|firstly, preparing a cylindrical sample with the diameter of 150mm and the height of 300mm according to the method of any one of claims 1-3;|cutting the cylindrical sample into two parts along the axial section of the cylindrical sample, exposing the section of the cylindrical sample, and acquiring images of the section; manually cutting the acquired image, and reserving an effective part;|binary conversion is carried out on the cut image, the picture type is converted into 8-bit from RGB, and noise reduction treatment is carried out at the same time, so that an analysis image is obtained;|cutting the analysis Image into 5 parts along the average, and introducing Image J software to perform identification and segmentation treatment on the internal polyphenyl particles;|and extracting the number and position distribution related information parameters of the polyphenyl particles in the image through software analysis and calculation. (CN116854421)|TECHNICAL FIELD|[0001] The invention relates to the field of building materials, in particular to recycling of building waste.|BACKGROUND ART|[0002] With the promotion of new construction, demolition and reconstruction projects of buildings generated by urban construction and related production activities, a large amount of building wastes are generated, and the amount of waste concrete is increased gradually, and the annual growth speed is 5% -10%. The construction wastes cannot be recovered and cleared in time, so that the construction wastes cause a certain harm to the environment and limit the development speed of cities. With the continuous development of natural resources and the increase of the quantity of wastes, the sustainable utilization and management of the construction wastes have profound significance for the green development of the future construction industry.|[0003] The construction waste mainly comprises waste concrete, wherein the concrete comprises natural river sand, broken stone, cement, cementing material and various additives. After the discarded concrete is crushed, recycled concrete coarse aggregate (RCA), recycled concrete fine aggregate (RFA) and recycled micro powder (RCP) with the particle size meeting the relevant specifications can be obtained. The recycled aggregate mainly comprises 65-70% of natural aggregate and 30-35% of adhesive mortar by volume, and compared with the natural aggregate, most recycled aggregate has smaller density, more surface edges and corners and larger roughness. Meanwhile, due to the complex interface transition condition of the recycled aggregate, more or less cement mortar components exist on the crushed aggregate, and certain cracks can be generated on the aggregate in the mechanical treatment process, so that the physical properties of the recycled aggregate are weaker than those of the natural aggregate, and the recycled aggregate has higher porosity, water absorption and crushing indexes, thereby limiting the application of the recycled concrete as a bearing structure. The development of recycled concrete in the future will thus be mainly in terms of non-load-bearing structures. |[0004] Polystyrene particles (Expanded Polystyrene, EPS) are produced and used in large quantities as a high molecular petroleum compound material, and the polystyrene particles have the characteristics of light weight, heat preservation, heat insulation, sound insulation, moisture resistance and the like as a light foam wallboard material, and are widely applied as non-bearing structures in assembled buildings.|[0005] Therefore, the recycled concrete is expected to have a certain application prospect in the field of polystyrene particle wallboards.|DISCLOSURE|Disclosure of Invention|[0006] The invention adopts the method that the recycled fine aggregate is carbonized and modified and then is combined with the polystyrene particle material to prepare the carbonized recycled fine aggregate polystyrene concrete meeting the requirements of relevant standards, expands a new way of recycling and industrialization application of solid waste of buildings and popularizes the application of the recycled fine aggregate in engineering practice.|[0007] The main technical scheme adopted by the invention is as follows:|[0008] a method for preparing polyphenyl granule concrete by using carbonized regenerated fine aggregate is characterized by comprising the following steps:|[0009] step one, preparing recycled fine aggregate;|[0010] crushing the waste concrete blocks to obtain recycled fine aggregate;|[0011] firstly, stripping steel bars from waste concrete to obtain waste concrete blocks, primarily crushing to obtain 25-50mm recycled coarse aggregate, crushing by a jaw crusher, and screening by a vibrating screen to obtain recycled fine aggregate; |[0012] Step two, putting the regenerated fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; CO is introduced again 2 The pressure in the carbonization furnace is 0.1-0.4MPa, and carbonization is carried out for 12-48 hours to obtain carbonized fine aggregate;|[0013] step three, 600:240-360:120-240: and mixing cement, river sand, carbonized fine aggregate and EPS particles uniformly in a mass ratio of 7.5, and adding water according to a water-cement ratio of 0.46, and mixing uniformly.|DRAWINGS DESCRIPTION|[0014] FIG. 1 is a schematic view showing the structure of a carbonization furnace in example 2;|[0015] FIG. 2 is a top view of FIG. 1;|[0016] fig. 3 is a schematic view of the structure of the support plate 32;|[0017] FIG. 4 is a graph showing the effect of carbonization time-pressure on apparent density of aggregate corresponding to example 3;|[0018] FIG. 5 is a graph showing the effect of carbonization time-pressure on bulk density of aggregate corresponding to example 3;|[0019] FIG. 6 is a graph showing the effect of carbonization time-pressure on the close packing density of aggregates corresponding to example 3;|[0020] FIG. 7 is a graph showing the effect of carbonization time-pressure on aggregate saturation and dry water absorption for example 3;|[0021] FIG. 8 is a graph showing the influence of carbonization time-pressure on aggregate crushing index corresponding to example 3;|[0022] FIG. 9 is a graph showing the effect of carbonization time-pressure on aggregate pH corresponding to example 3;|[0023] FIG. 10 is a microscopic morphology of the non-carbonized recycled fine aggregate corresponding to example 3; |[0024] FIG. 11 is a graph of the microtopography of the carbonized aggregate corresponding to example 3;|[0025] FIG. 12 is an XRD diffraction pattern of carbonized aggregates at the same carbonization pressure and at different carbonization times corresponding to example 3;|[0026] FIG. 13 is an XRD diffraction pattern of carbonized aggregates at different carbonization pressures at the same carbonization time corresponding to example 3;|[0027] FIG. 14 is a graph of TG curve corresponding to example 3;|[0028] FIG. 15 is a graph of the corresponding DTG of example 3;|[0029] FIG. 16 is a plot of dry concrete density versus substitution for example 4;|[0030] FIG. 17 is a graph showing the water absorption of concrete under different carbonization conditions-substitution rate according to example 4|[0031] FIG. 18 is a concrete slump-displacement ratio bar chart corresponding to example 4;|[0032] FIG. 19 is a bar graph of compressive strength corresponding to example 4;|[0033] FIG. 20 is a bar graph of the split tensile strength corresponding to example 4.|INVENTION MODE|Detailed Description|[0034] The invention is further described below with reference to examples and figures.|[0035] Example 1:|[0036] the preparation process of polyphenyl granule concrete with carbonized regenerated fine aggregate includes the following steps:|[0037] step one, preparing recycled fine aggregate;|[0038] the test is selected from column and beam structural members of civil buildings in a brick-concrete structure, firstly, stripping reinforcing steel bars from waste concrete, primarily crushing the waste concrete by manpower or a machine to obtain regenerated coarse aggregate with the diameter of 25-50mm, then crushing the waste concrete by a jaw crusher, removing impurity components such as wood dust, iron wires and the like, and screening the waste concrete by a vibration screening machine to obtain regenerated fine aggregates with different particle diameters; |[0039] Step two, putting the regenerated fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; CO is introduced again 2 The pressure in the carbonization furnace is 0.1-0.4MPa, and carbonization is carried out for 12-48 hours to obtain carbonized fine aggregate;|[0040] for carbonization reaction of the aggregate, the small water content of the aggregate can lead to the incapability of timely dissolving carbon dioxide gas to participate in carbonation reaction, the large water content can lead to the aggregation phenomenon of water on the surface of the aggregate, and a large amount of calcium ions overflow the outer surface of the aggregate to not timely participate in carbonation reaction to influence the porosity of the aggregate, so that the proper water content of the aggregate is beneficial to the carbonization reaction.|[0041] Therefore, before carbonization, the recycled fine aggregate is preferably placed in an indoor environment at a temperature of 23 ℃ and a humidity of 45 to 55% for 7 days, and then placed in a carbonization furnace to be carbonized.|[0042] In a further preferred embodiment, in the second step, CO is introduced into the carbonization furnace 2 Until the pressure is 0.4MPa, the carbonization time is 48h.|[0043] Step three, 600:240-360:120-240: and mixing cement, river sand, carbonized fine aggregate and EPS particles uniformly in a mass ratio of 7.5, and adding water according to a water-cement ratio of 0.46, and mixing uniformly. |[0044] Example 2:|[0045] as shown in fig. 1, 2 and 3, the carbonization furnace comprises a tank body 1 and a tank cover 2 which is buckled on the tank body 1 in a sealing way, wherein the tank body 1 and the tank cover 2 are respectively provided with flanges which are matched with each other, and holes for connecting bolts are arranged on the flanges; at least three support legs 4 are arranged on the outer wall of the tank body 1. The support legs 4 overhead the tank body 1;|[0046] the bottom of the inner wall of the tank body 1 is an arc-shaped surface, the concave surface of the arc-shaped surface faces upwards, and the bottom of the tank body 1 is connected with a drain pipe 11 and CO 2 An air inlet pipe 12, said CO 2 The air inlet pipe 12 is vertically arranged, and the CO 2 The upper part of the air inlet pipe 12 extends into the tank body 1, and the CO 2 The upper end port of the air inlet pipe 12 is closed, and the CO is formed by 2 A lateral air inlet is arranged on the upper pipe wall of the air inlet pipe 12, and a negative pressure suction pipe 13 is connected to the upper part of the tank body 1; a drain valve is arranged on the drain pipe 11, and the CO is arranged on the drain pipe 2 The air inlet pipe 12 is provided with a pressure reducing valve;|[0047] the sewage drain pipe 11 is vertically arranged, the upper end of the sewage drain pipe 11 is connected with the lowest part of the arc-shaped surface, and the pipe orifice at the upper end of the sewage drain pipe 11 is communicated with the tank body 1; a pipe orifice blocking cover 14 is arranged in the tank body 1 corresponding to the upper end of the sewage drain pipe 11, the pipe orifice blocking cover 14 is buckled at the bottom of the tank body 1, the edge of the pipe orifice blocking cover 14 is fixedly connected with the inner wall of the tank body 1, and a plurality of small holes are formed in the pipe orifice blocking cover 14; |[0048] The tank cover 2 is provided with a thermometer 21, a safety valve 22 and an emptying pipe 23, and the emptying pipe 23 is provided with a pressure gauge.|[0049] A plurality of supporting tray components are vertically distributed in the tank body 1; the support tray assembly comprises at least three support blocks 31 and one support disc 32, wherein the support blocks 31 are fixed on the inner wall of the tank body 1, the support discs 32 are tiled in the tank body 1, the edges of the support discs 32 are lapped on the corresponding support blocks 31, and the edges of the support discs 32 are provided with yielding notches which correspond to the support blocks 31 one by one;|[0050] the support plate 32 may be of a fine mesh structure so that recycled fine aggregate is directly stacked thereon; the support plate 32 may have a coarse mesh structure, and the regenerated fine aggregate may be contained in a net bag and placed on the support plate 32.|[0051] Example 3:|[0052] selecting the same batch of recycled fine aggregate, randomly dividing the recycled fine aggregate into a plurality of parts, and carbonizing the recycled fine aggregate according to the parameter configuration of the following table 1:|[0053] TABLE 1 carbonization parameters of recycled fine aggregate|[0054] |[0055] According to the standard GB/T14684-2011, the aggregate density (including apparent density, loose bulk density and close bulk density), saturated surface dry water absorption, crushing index and pH of each group of carbonized fine aggregates are measured and compared with those of the original non-carbonized regenerated fine aggregates, and the results are shown in figures 4-9; |[0056] As can be seen from fig. 4, 5, 6: the density of the recycled fine aggregate can be increased by carbonization treatment. Compared with the regenerated fine aggregate which is not subjected to carbonization pretreatment, the carbonization pressure is increased from 0.1MPa to 0.4MPa under the same carbonization time treatment condition, and the apparent density is improved. The apparent density of the aggregate after 24 hours of treatment under the pressure of 0.1MPa is less than 0.2MPa and 0.4MPa, which is probably caused byUnder the condition of low pressure of 0.1MPa, calcium carbonate and other carbonization reaction products generated by the reaction of carbon dioxide with moisture, calcium hydroxide and other substances in the pores on the surface of the aggregate block the subsequent gas from entering the aggregate, so that the carbonization reaction degree of the subsequent aggregate is reduced, and the apparent density improvement effect of the aggregate under the carbonization condition is not good. With the increase of carbonization pressure from 0.1MPa to 0.2MPa and 0.4MPa, the apparent density can be increased by 27.51-94.13kg/m 3 . Has optimal carbonization effect under the condition of 0.4MPa, and has the maximum apparent density of 2650.42kg/m 3 。|[0057] Compared with the regenerated fine aggregate which is not subjected to carbonization pretreatment, under the same carbonization pressure treatment condition, the carbonization time is increased from 12h to 24h and 48h, and the apparent density is increased by 8.62-127.50kg/m 3 . Has the maximum improving effect under the condition of 48 hours, and the maximum apparent density is 2683.79kg/m 3 。|[0058] For loose bulk density, the influence of different carbonization pressures is small, and the bulk density after pretreatment for 24 hours under the pressure of 0.4MPa is only increased by 14.94kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The maximum bulk density after pretreatment under the conditions of 0.4MPa pressure and different carbonization times is only increased by 17.44kg/m 3 . For the compact bulk density, the apparent density can be increased by 76.1-114.56kg/m with increasing carbonization pressure from 0.1MPa to 0.2MPa and 0.4MPa 3 Compared with the recycled fine aggregate which is not subjected to carbonization pretreatment, the recycled fine aggregate is improved by 5.73 percent, 6.37 percent and 8.63 percent respectively, and the bulk density under the carbonization treatment condition of 0.4MPa-24h is the maximum and is 1442.13kg/m 3 . As the carbonization time increases from 12h to 24h and 48h, the close packing density can increase from 94.63 kg/m to 138.00kg/m 3 Compared with the recycled fine aggregate which is not subjected to carbonization pretreatment, the recycled fine aggregate is improved by 7.13 percent, 8.63 percent and 10.39 percent respectively, and the bulk density under the carbonization treatment condition of 0.4MPa to 48h is the maximum and is 1465.57kg/m 3 . The carbonization reaction generates calcium carbonate and other carbonization reaction products, so that the surface pores of the aggregate are filled and the aggregate is densified, and the mass fraction of the regenerated fine aggregate is larger under the condition of the same volume unit. Has similar conclusion with apparent density as carbonization The increase in the number of the elements increases the effect of carbonization on improving the bulk density of the recycled fine aggregate.|[0059] As can be seen from fig. 7: under the same carbonization time condition, the water absorption of the recycled fine aggregate shows a decreasing trend along with the increase of carbonization pressure, the carbonization pressure is increased from 0.1MPa to 0.2MPa and 0.4MPa, the water absorption of the recycled fine aggregate is respectively decreased by 16.97%, 24.51% and 29.31%, wherein the carbonization pressure with the best water absorption improvement effect on the recycled fine aggregate is 0.4MPa, and the water absorption of the aggregate is 7.50%. Under the same carbonization pressure, the water absorption of the recycled fine aggregate shows a decreasing trend along with the increase of the carbonization time, the carbonization time is increased from 12h to 24h and 48h, the water absorption of the recycled fine aggregate is respectively decreased by 15.55%, 29.31% and 31.67%, wherein the carbonization time with the largest water absorption improvement effect on the recycled fine aggregate is 48h, and the water absorption of the aggregate is 7.25%. The best carbonization condition of the test has 31.67 percent of water absorption reduction effect on the recycled fine aggregate.|[0060] As can be seen from fig. 8: the crushing index value of the recycled fine aggregate subjected to carbonization pretreatment is smaller than that of the recycled fine aggregate not subjected to carbonization pretreatment. Under the same carbonization time condition, the crushing index value of the recycled aggregate shows a decreasing trend along with the increase of carbonization pressure. When the carbonization time is controlled to be 24 hours, the carbonization pressure is increased from 0.1MPa to 0.2MPa and 0.4MPa, the crushing index values are respectively reduced by 3.23%, 6.45% and 19.35% compared with the crushing index values of the recycled aggregate which is not subjected to carbonization pretreatment, and the minimum crushing index value of the recycled aggregate subjected to carbonization treatment under the condition of 24 hours to 0.4MPa is 25%. Under the same carbonization pressure, the crushing index value of the recycled aggregate shows a decreasing trend with the increase of carbonization time. When the carbonization pressure is controlled to be 0.4MPa, after the carbonization time is increased from 12h to 24h and 48h, the crushing index values are respectively reduced by 9.68%, 19.35% and 25.81%, and the minimum crushing index value of the recycled aggregate subjected to carbonization treatment under the condition of 48h-0.4MPa is 23%. The carbonization pretreatment can effectively reduce the crushing index of the recycled aggregate. The carbonization pretreatment has the improvement effect on the crushing index of the recycled aggregate, mainly calcium carbonate crystals and other carbonization reaction products are produced through carbonation reaction, so that the surface micro-pore structure of the fine aggregate is filled, the strength grade of the aggregate is improved to a certain extent, and compared with the recycled aggregate which is not subjected to carbonization treatment, the recycled aggregate has a larger strength value, and the crushing index value is reduced. |[0061] As can be seen from fig. 9: under the same carbonization time conditions, it was found that the water absorption of the recycled fine aggregate showed a decreasing trend with increasing carbonization pressure. After the carbonization pressure is increased from 0.1MPa to 0.2MPa and 0.4MPa, the pH value of the recycled fine aggregate is respectively reduced by 24.75%, 27.68% and 28.52%, wherein the carbonization pressure with the best effect on improving the pH value of the recycled fine aggregate is 0.4MPa, and the pH value of the aggregate is 8.52. Under the same carbonization pressure, the pH value of the recycled fine aggregate was found to show a decreasing trend with increasing carbonization time. After the carbonization time is increased from 12h to 24h and 48h, the pH value of the recycled fine aggregate is respectively reduced by 24.66%, 28.52% and 28.86%, wherein the carbonization time with the best effect on improving the pH value of the recycled fine aggregate is 48h, and the pH value of the aggregate is 8.48.|[0062] The microscopic morphology of the surface of the regenerated fine aggregate and the carbonized aggregate is observed by a scanning electron microscope, and the results are shown in fig. 10 and 11 respectively.|[0063] As shown in fig. 10, the mortar component structure on the surface of the recycled fine aggregate which is not subjected to carbonization pretreatment is observed to be loose, a more obvious wide gap exists, and the interface transition zone of the recycled aggregate which is subjected to carbonization pretreatment in fig. 11 is observed to be more compact. The uncarbonized cement mortar has a loose and porous structure, and a large amount of white substances are distributed on the surface. The surface of carbonized cement slurry is found to contain a large amount of white granular matters agglomerated, the overall structure is remarkably tighter than that of the uncarbonated slurry, the pore structure is remarkably reduced, and a plurality of larger pores are gradually filled with matters generated by carbonization reaction to become smaller pore structures. This is mainly due to: on one hand, carbon dioxide enters the surface pores of the recycled aggregate and is dissolved in water, and then the carbon dioxide and calcium hydroxide in mortar generate carbonization reaction, so that carbonization reaction products such as calcium carbonate, silica gel and the like are filled in the surface pore structures of the recycled fine aggregate in microcracks, and the interface structure of the recycled fine aggregate is densified, so that the physical property of the recycled fine aggregate is improved. Meanwhile, a certain amount of needle-shaped ettringite crystals and C-S-H cementing materials are mutually interwoven in the mortar, but the mortar has more pore structures and larger gaps exist in an interface transition zone. On the other hand, certain regenerated micro powder exists on the surface of the regenerated fine aggregate, and the regenerated micro powder not only can play a role in filling gaps in the hydration process, but also can play a certain role in pozzolanic effect, so that more hydration products are generated in the interface transition zone, and the interface transition zone is improved to a certain extent. |[0064] The diffraction patterns of carbonized aggregates under the conditions of increasing carbonization time from 12h to 24h and 48h under the same carbonization pressure of 0.4MPa are respectively measured by adopting an XRD diffractometer, and the result is shown in figure 12;|[0065] under the same carbonization time condition of 24 hours, the diffraction patterns of carbonized aggregate when the carbonization pressure is increased from 0.1MPa to 0.2MPa and 0.4MPa are shown in the result of FIG. 13;|[0066] fig. 12 and 13 reflect the variation of diffraction peak intensity for recycled fine aggregates under different carbonization conditions. It can be seen that: after carbonization treatment, the diffraction peak intensity of calcium hydroxide and ettringite is obviously reduced, and the diffraction peak intensity of calcium carbonate is obviously increased.|[0067] Under the same carbonization pressure of 0.4MPa, the carbonization time is increased from 12h to 24h and 48h, and the intensity of the calcium carbonate diffraction peak is slightly increased but not obvious. However, when the pressure was increased from 0.1MPa to 0.2MPa or 0.4MPa with respect to the fixed 24-hour period, the diffraction peak was observed to be increased.|[0068] The TG curve and DTG curve under different carbonization conditions were measured, and the results are shown in fig. 14 and 15, respectively, and it can be seen from fig. 14 and 15: the first peak value change interval is 5-200 ℃, and the contrast shows that the mass loss difference in the range is more obvious, the quality change of untreated recycled aggregate is 7.43%, and the mass loss after carbonization treatment is only 1.98%. Mainly caused by the water decomposition of the bound water in hydration products such as calcium aluminate hydrate, AFt, C-S-H and the like which are contained in a certain amount in the raw aggregate. The second peak change lies in the range of 350-550 c, which is primarily the decomposition of the calcium hydroxide product. The obvious difference of the change condition of calcium hydroxide substances before and after carbonization is observed, which is mainly caused by the consumption of calcium hydroxide in the aggregate by carbonization reaction, and the quality loss of the aggregate after carbonization treatment is only 0.91 percent at most. The third peak change is in the range of 550-800 ℃, and the mass change degree is found to be more different, especially the mass loss of aggregate before and after carbonization. With increasing carbonization time, the mass loss was 39.69%, 44.92% and 48.67% in order; as the carbonization pressure increases, the mass loss is 39.17%, 39.87% and 44.92% in sequence; the quality loss of the regenerated fine aggregate which is not subjected to carbonization pretreatment is only 10.27%, and the carbonization treatment remarkably changes the quality change condition within the range of 550-800 ℃. The loss of quality may be due to the formation of calcium carbonate species of varying degrees of crystallization. The loss of calcium carbonate crystal decomposition in the range of 550 to 700 ℃ is considered to be poor in crystallization, and the mass change caused by calcium carbonate decomposition in the range of 700 to 800 ℃ is mainly good in crystallization. The conclusion is similar to XRD test results, and indicates that under the condition of a certain carbonization pressure, the carbonization reaction product generated by early carbonization reaction can effectively improve the pore structure of the surface of the aggregate, reduce the water absorption and enhance the performance of the aggregate. On the other hand, however, the calcium carbonate formed by the method and the corresponding carbonization reaction products are densified on the surface of the aggregate, and the carbon dioxide gas is prevented from entering and participating in the subsequent reaction, so that the difference of mass loss is not significant as carbonization time is increased in the figure. |[0069] And (3) carbonization mechanism analysis of the recycled fine aggregate: when carbonization reaction occurs, carbon dioxide gas firstly enters the surface and the inside of the aggregate, and is dissolved in the water of the aggregate to form carbonic acid. As the carbonation reaction proceeds, the pH of the solution in the original pores of the aggregate changes and becomes neutral. The ettringite (AFt), monosulfate (AFm), calcium hydroxide and other related substances in the raw mortar can be subjected to carbonization reaction. At ph=11.6, AFm begins to decompose to form alumina and AFt; at ph=10.6, AFt begins to decompose to form sulfate and hydroxide ions, providing a starting material for subsequent carbonization reactions. The carbonic acid and the calcium hydroxide in the mortar of the raw aggregate are subjected to carbonation reaction to generate calcium carbonate crystals, the calcium carbonate generated by the reaction exists in three forms of aragonite, vaterite and calcite, and the calcium carbonate is finally converted into calcite with good crystallization and exists stably. The C-S-H and other carbonizable substances also react with carbon dioxide to generate a certain content of calcium carbonate and gelled substances, and the gelled substances and calcium carbonate crystals generated by calcium hydroxide are clustered together and grow into blocks and adhere to the outer surface of the aggregate and the interface transition zone, so that the density of the aggregate is increased, and the water absorption rate of the aggregate is reduced. The carbonization mechanism can obviously improve the apparent density of the aggregate in early stage, and reduce the water absorption rate by 15.55% -31.67%; reducing the crushing index by 3.23-25.81%; the pH value is reduced by 24.66% -28.86%. However, when the carbonization condition is further changed, the carbonization time is increased, and the carbonization pressure is increased, it is found that the carbonization gain effect is gradually decreased. The early carbonization gain is mainly used for enabling generated carbonization reaction products to be attached to the surface of the aggregate and forming a relatively dense film in an interface transition zone, so that the subsequent carbonization reaction is prevented from being generated when carbon dioxide gas enters into gaps of the aggregate. |[0070] Example 4:|[0071] based on each carbonized aggregate (C1T 24, C2T24, C4T12, C4T24, C4T 48) obtained in example 3, polyphenyl granular concrete was prepared in the following proportions of table 2:|[0072] TABLE 2 polyphenyl granule concrete formulation Table (kg/m) 3 )|[0073] |[0074] In Table 2, the amount of river sand was 480kg/m based on the N group of non-recycled fine aggregate/carbonized aggregate 3 The method comprises the steps of carrying out a first treatment on the surface of the Replacing part/all river sand with recycled fine aggregate/carbonized aggregate according to different substitution rates (25%, 50%, 75%, 100%);|[0075] substitution rate= (amount of recycled fine aggregate/amount of carbonized aggregate)/480 x 100%.|[0076] According to GB/T50081-2019 Standard of method for testing physical and mechanical properties of common concrete, concrete with various proportions in Table 2 is used as a raw material, and a standard test piece of polystyrene particle recycled fine aggregate concrete with the dimensions of 100mm multiplied by 100mm is prepared by test design to test the mechanical properties of the concrete. Because the recycled fine aggregate has higher aggregate water absorption rate, saturated water absorption treatment is needed to avoid the influence of the local water-cement ratio difference of concrete caused by direct water addition when the concrete is prepared, and thus the concrete is needed to be prepared according to the preparation flow of the figure. Firstly, uniformly stirring natural aggregate and regenerated fine aggregate, putting 1/3 of water into the mixture to saturate the mixture, stirring the mixture for 2 minutes, putting cement and the rest 1/2 of water into the mixture to stir the mixture for 3 minutes, finally, adding the rest of water into the mixture to stir the mixture for 3 minutes, and uniformly putting EPS particles into the mixture to stir the mixture for 5 minutes after the cement is fully stirred. And then the uniformly mixed concrete material is layered and placed into a steel test die, and is uniformly distributed by adopting a manual insertion and tamping mode, and is put into the die, and then is subjected to film coating treatment in time, and is subjected to demoulding treatment after being cured for 24 hours in an environment with the relative humidity of more than 50 percent at 20+/-5 ℃, and the samples are separated from each other by 10-20mm and are placed into a standard constant temperature and humidity curing box with the relative humidity of more than 95 percent at 20+/-2 ℃ for standard curing. And (5) after 28d standard curing, taking out in time, and putting into an infrared blast drying oven with the temperature of 105+/-5 ℃ for drying treatment, and keeping for later use. |[0077] The dry density of the concrete was tested with reference to specification GB/T50081-2019, the results being shown in FIG. 16;|[0078] as can be seen from fig. 16, as the substitution rate of recycled aggregate increases, the dry density of the recycled fine aggregate polyphenyl granule concrete decreases. When the substitution rate of the recycled fine aggregate is increased from 25% to 100%, the dry density thereof is increased from 1323.83g/cm 3 Reduced to 1311.37g/cm 3 The method comprises the steps of carrying out a first treatment on the surface of the When the C4T24 carbonized regenerated fine aggregate is adopted, the dry density of the concrete adopting the carbonized regenerated fine aggregate is from 1339.97g/cm 3 Reduced to 1318.10g/cm 3 . The carbonization pretreatment improves the dry density value of the concrete, but the improvement effect is not obvious, and the maximum dry density value of the concrete is improved by 1.22 percent only under the condition of 25 percent substitution rate. When the C4T48 carbonization is adopted to regenerate the fine aggregate, the dry density of the concrete is 1346.23g/cm 3 Reduced to 1320.86g/cm 3 The density increase was slightly higher than that of the C4T24 control, again increasing by a maximum of 1.69% at 25% substitution. Carbonization timeThe increase of the density of the concrete is achieved, the lifting effect is derived from carbonization pretreatment, so that the apparent density of the recycled fine aggregate is increased, and the surface of the carbonized recycled aggregate has more calcium carbonate crystals and carbonization reaction products in the same volume state, so that the mass fraction of the aggregate is increased, and the dry density value of the concrete is further improved. |[0079] The water absorption of concrete was tested with reference to specification GB/T50081-2019 and the results are shown in FIG. 17. The RCA in fig. 17 includes four sets of water absorption rates R25, R50, R75, R100 in table 2; C4T24 includes four sets of water absorption in table 2, C4T24R25, C4T24R50, C4T24R75, C4T24R 100; the C4T48 includes four sets of water absorption rates C4T48R25, C4T48R50, C4T48R75, C4T48R100 in Table 2. As can be seen from fig. 17, the water absorption of the recycled fine aggregate concrete without carbonization pretreatment is generally higher than that of the carbonized group. Wherein the water absorption of the concrete after 24 hours carbonization pretreatment is reduced by 35.49%, 34.97%, 29.13% and 23.29% respectively compared with the non-carbonized control group, and the concrete has the minimum water absorption value of 10.99% when the fine aggregate substitution rate is 25%. As carbonization time increases from 24h to 48h, the concrete water absorption value shows a decreasing trend, but the change degree is not significant, and the water absorption value is respectively decreased by 5.88%, 4.00%, 4.33% and 5.65% under different substitution rate conditions relative to a 24h carbonization group. Due to the presence of the carbonization reaction inhibition, the water absorption rate increases with the increase of the carbonization time under the same carbonization conditions, but the improvement effect thereof is not significant.|[0080] Slump of concrete was tested with reference to specification GB/T50080-2002, the results being shown in FIG. 18; |[0081] According to the concrete slump test result shown in fig. 18, in the case where the cement ratio is the same, as the substitution rate of the recycled fine aggregate increases, the fluidity of the concrete decreases, and the slump decreases, wherein the slump is only 116mm under the substitution rate of 100% of the total recycled aggregate, and the slump is decreased by 38.95% compared with the natural control group. After carbonization pretreatment, the fluidity of the concrete is improved, and the slump of the concrete is improved by the carbonization pretreatment of the recycled fine aggregate. The improvement effect of the recycled fine aggregate under the carbonization treatment condition of C4T24 is smaller at the low substitution rate of 0-50%, which is 185mm and 180mm respectively; the improvement effect is obvious under the condition of 50-100% substitution rate, and the flowability under the condition of 75% and 100% regeneration fine aggregate substitution rate is 167mm and 149mm. Compared with a control group without carbonization treatment, the 100% of the fully regenerated carbonized regenerated fine aggregate concrete has 28.45% of improved performance.|[0082] The improvement effect of the recycled fine aggregate under the carbonization treatment condition of C4T48 is observed to be smaller at a low substitution rate of 25%, which is 187mm; the improvement effect is obvious under the condition of 50-100% substitution rate, and the flowability under the condition of 50%, 75% and 100% regeneration fine aggregate substitution rate is 184mm, 175mm and 156mm. Compared with a control group without carbonization treatment, the 50% of the fully regenerated carbonized regenerated fine aggregate concrete has the performance improved by 40.00%. |[0083] The working performance analysis of the regenerated fine aggregate control group treated under the same pressure condition and different carbonization time shows that the regenerated fine aggregate group carbonized for 48 hours has a larger slump value, and compared with the 24-hour carbonized group, the regenerated fine aggregate control group has different degrees of improvement of 1.08-4.79 percent under the condition of 25-100 percent substitution rate, and has larger flow performance under the condition of the same water cement ratio.|[0084] The recycled aggregate which is not carbonized is extremely easy to cause more edges and corners on the surface of the aggregate, microcracks and the existence of recycled micro powder, mud blocks and other substances in the crushing process, so that the water demand of the concrete is increased, and the free water in the concrete using the recycled fine aggregate is reduced under the condition of the same water-cement ratio, thereby reducing the flowability of the concrete. The improvement of the fluidity is mainly beneficial to the carbonization reaction, so that compact calcium carbonate crystal components can be formed on the surface of the aggregate to fill the pores, the water absorption rate of the recycled aggregate is reduced, more free water on the surface of the aggregate can exist in the concrete preparation process, and the fluidity of the mixture is greatly increased.|[0085] The concrete cubes were tested for compressive strength with reference to specification GB/T50081-2019, the results being shown in FIG. 19; |[0086] As can be seen in connection with fig. 19, the concrete using the recycled fine aggregate has lower overall strength than the control group using the natural river sand aggregate, which is mainly caused by the recycled fine aggregate attaching mortar and the self-void structure. The recycled fine aggregate contains a large amount of waste mortar, has lower strength, and generates a larger interface transition area when the recycled fine aggregate is combined with the new mortar to form concrete, so that the compressive strength of the concrete is lower than that of common concrete. Meanwhile, a large number of microcracks exist on the recycled fine aggregate after the recycled fine aggregate is treated in a mechanical crushing mode, and the compressive strength of the concrete is also adversely affected. In addition, the fact that the machine-made sand grading adopted by the recycled fine aggregate is different from the natural river sand to a certain extent is considered, and the components such as micro powder, mortar and the like in the recycled fine aggregate can absorb certain moisture in the concrete preparation process to cause local water-cement ratio change, so that the hydration of the cement is prevented from influencing the strength increase of the concrete.|[0087] The compressive strength of the concrete generally tends to decrease with increasing substitution rate of the recycled fine aggregate, wherein the compressive strength of the concrete using the recycled fine aggregate is lower than that of the concrete of the common control group using the natural aggregate. Meanwhile, the concrete adopting the carbonized regenerated fine aggregate is generally higher than the concrete control group which is not carbonized, which benefits from accelerating carbonization to generate a large amount of calcium carbonate crystals and other reaction products, and the concrete has a strengthening effect on the whole of the original regenerated aggregate and the attached mortar. |[0088] The recycled fine aggregate concrete has a similar strength development rule with the common concrete, the compressive strength of the recycled fine aggregate concrete shows a growth trend along with the increase of curing time, and the early strength of the concrete is obviously increased in 3-7d compared with 7-28 d. The strength of the concrete which adopts the recycled fine aggregate without carbonization pretreatment is increased by 4.88% -9.15% in the early stage of 3-7d, wherein the strength is increased to the maximum of 9.15% when the substitution rate is 50%; the increase in strength was 3.46% -8.63% at early 7-28d, with a maximum increase in strength of 8.63% at a substitution rate of 50%. The carbonization pretreatment obviously improves the change condition of the growth, the strength of the concrete adopting the C4T24 carbonized regenerated fine aggregate can reach 7.36-13.16% in early 3-7d, wherein the strength can reach 13.16% at maximum when the substitution rate is 50%; the strength increase can reach 6.97% -11.74% in 7-28d, wherein the maximum strength increase can reach 11.74% under the condition of 50% substitution rate. The strength of the concrete adopting the C4T48 carbonized and regenerated fine aggregate can reach 11.00% -13.76% in early 3-7d, wherein the maximum strength increase can reach 13.16% when the substitution rate is 50%; the strength increase can reach 6.97% -11.74% in 7-28d, wherein the maximum strength increase can reach 11.74% under the condition of 50% substitution rate. |[0089] Comparing the recycled fine aggregate concrete which is not carbonized and pretreated in the same period with the recycled fine aggregate concrete which is carbonized and treated under different conditions, the method has the following advantages that: the concrete pretreated by C4T24 carbonization has the improvement effect of 0.38-2.68%, 2.74-5.88% and 5.33-7.49% of compressive strength respectively at 3d, 7d and 28d, and the maximum compressive strength value is 9.61MPa. The strength improvement effect of the C4T24 on concrete is mainly between 3 and 28 days, and the strength improvement effect of the C4T24 on 3 days is not remarkable. The compressive strength of the concrete pretreated by C4T48 carbonization is respectively improved by 1.25 to 8.89 percent, 6.52 to 13.49 percent and 5.45 to 9.62 percent at 3d, 7d and 28 d. The improvement effect is superior to that of a carbonization control group for 24 hours under the same carbonization pressure, wherein the strength increase under the condition of 50 percent substitution rate is 8.89 percent, 13.49 percent and 9.62 percent respectively, and the maximum compressive strength is 9.80MPa. It is therefore recommended that the optimum recycled fine aggregate substitution rate be 50%.|[0090] After carbonization treatment, the compressive strength of the concrete is obviously improved. The carbonization technology is beneficial to the improvement of the pore structure of the recycled fine aggregate by generating a large amount of calcium carbonate crystals in the recycled fine aggregate, so that the recycled fine aggregate is more densified. The carbonization reaction product and the hydration reaction product can effectively fill the interface transition area between the recycled aggregate and the new mortar, thereby improving the compressive strength of the concrete. However, the improvement and improvement effect of the carbonization time from 24h to 48h on the compressive strength of the concrete is not obvious, and the compressive strength of the 28d concrete is only improved by 0.11% -1.98% when the compressive strengths of two different carbonization conditions are compared. Under the same carbonization pressure conditions, the improvement of the compressive strength is not obvious as the carbonization time increases from 24h to 48 h. |[0091] This also explains from another aspect that the carbonization effect is affected by the carbonization time so that the carbonization effect does not show an increasing trend with time to some extent, the improvement effect thereof is affected by the improvement of early carbonization, so that the later carbonization time increases but the subsequent carbon dioxide cannot sufficiently enter the inside of the recycled aggregate to provide the carbonization reaction raw material so that the improvement effect gradually declines. The optimal carbonization time is therefore recommended to be 24h.|[0092] The concrete split tensile strength was tested according to GB/T50081-2019 and the results are shown in FIG. 20;|[0093] as shown in fig. 20, the concrete using recycled aggregate has significantly lower split tensile strength than concrete using natural river sand as fine aggregate. With the increase of the substitution rate of the recycled aggregate, the splitting tensile strength of the concrete gradually decreases, but the carbonization pretreatment improves the strength of the concrete. As the substitution rate increases, the split tensile strength of the recycled fine aggregate concrete is reduced by 9.40%, 16.98%, 23.23% and 32.45% respectively compared with the natural river sand concrete control; the concrete reduction levels using the carbonized recycled fine aggregate were 7.26%, 16.04%, 22.73% and 25.0%, respectively. The carbonization treatment improves the splitting tensile strength of the recycled concrete by 0.53-8.09%, wherein the improvement effect of the recycled concrete on 100% of the fully recycled fine aggregate concrete is optimal and reaches 8.09%. It is therefore recommended that the optimum recycled fine aggregate substitution rate be 25%. Mechanism analysis: the splitting tensile strength of the recycled fine aggregate concrete is lower than that of the natural fine aggregate concrete control group, and the splitting tensile strength of the recycled fine aggregate concrete subjected to carbonization pretreatment is higher than that of the recycled fine aggregate concrete control group which is not subjected to treatment. Wherein, the splitting tensile strength of the recycled concrete shows a decreasing trend along with the increase of the substitution rate of the aggregate and the carbonized aggregate. The recycled aggregate consists of cement mortar and natural aggregate, wherein the recycled mortar has a larger pore structure and a larger water absorption rate. Meanwhile, the recycled fine aggregate contains more recycled micro powder, mud blocks and other substances in the preparation process, so that the water absorption of the recycled fine aggregate is increased, the free water consumption participating in hydration reaction in the mixing process is reduced, cement is hindered from participating in hydration reaction, the bonding degree of cement mortar and aggregate is reduced, and the splitting tensile strength of concrete is further influenced. After the recycled fine aggregate subjected to carbonization pretreatment is adopted, the splitting tensile strength of the recycled fine aggregate is improved. The carbonization effect produces a large amount of calcium carbonate crystals and carbonized products on the surface and in the pores of the aggregate, reduces the water demand of the recycled fine aggregate in the mixing process, ensures that more free water can exist in the mixing process to fully carry out hydration reaction with cement, increases the bonding capability of cement paste and the aggregate, and achieves the aim of improving the splitting tensile strength of the concrete. |[0094] Example 5:|[0095] a uniformity test method of polyphenyl granule concrete comprises the following steps:|[0096] according to GB/T50081-2019 "standard for test method of physical and mechanical properties of ordinary concrete", cylindrical samples with a diameter of 150mm and a height of 300mm were prepared according to the method of example 1, using concrete of each proportion in Table 2 as a raw material. Because the recycled fine aggregate has higher aggregate water absorption rate, saturated water absorption treatment is needed to avoid the influence of the local water-cement ratio difference of concrete caused by direct water addition when the concrete is prepared, and thus the concrete is needed to be prepared according to the preparation flow of the figure. Firstly, uniformly stirring natural aggregate and regenerated fine aggregate, putting 1/3 of water into the mixture to saturate the mixture, stirring the mixture for 2 minutes, putting cement and the rest 1/2 of water into the mixture to stir the mixture for 3 minutes, finally, adding the rest of water into the mixture to stir the mixture for 3 minutes, and uniformly putting EPS particles into the mixture to stir the mixture for 5 minutes after the cement is fully stirred. And then the uniformly mixed concrete material is layered and placed into a steel test die, and is uniformly distributed by adopting a manual insertion and tamping mode, and is put into the die, and then is subjected to film coating treatment in time, and is subjected to demoulding treatment after being cured for 24 hours in an environment with the relative humidity of more than 50 percent at 20+/-5 ℃, and the samples are separated from each other by 10-20mm and are placed into a standard constant temperature and humidity curing box with the relative humidity of more than 95 percent at 20+/-2 ℃ for standard curing. After 28d standard maintenance, taking out in time, and putting into an infrared blast drying oven with the temperature of 105+/-5 ℃ for drying treatment, and keeping for later use; |[0097] Cutting the cylindrical sample into two parts along the axial section of the cylindrical sample, exposing the section of the cylindrical sample, and acquiring images of the section; manually cutting the acquired image, and reserving an effective part;|[0098] binary conversion is carried out on the cut image, the picture type is converted into 8-bit from RGB, and noise reduction treatment is carried out at the same time, so that an analysis image is obtained;|[0099] cutting the analysis Image into 5 parts along the average, and introducing Image J software to perform identification and segmentation treatment on the internal polyphenyl particles;|[0100] and extracting the number and position distribution related information parameters of the polyphenyl particles in the image through software analysis and calculation.|[0101] Through researches on the uniformity distribution situation of polyphenyl particles in concrete under the conditions of different carbonization times of 24 hours and 48 hours and different substitution rates of 25%, 50%, 75% and 100% of recycled fine aggregates, the particle quantity uniformity index parameter of polyphenyl particle concrete of the recycled fine aggregates is generally lower than that of a natural river sand control group, and the main reasons are high water absorbability, irregular morphology and edges of the recycled fine aggregates.|[0102] The carbonized aggregate treated by carbonization effectively improves the distribution of polyphenyl particles in concrete, and in carbonized aggregate polyphenyl particle concrete, along with the increase of the aggregate substitution rate, the absolute values of various uniformity index parameters of the concrete are in a decreasing trend. The carbonization treatment fills the pore structure on the surface of the aggregate, and reduces the water absorption rate of the aggregate. Under the same water-cement ratio condition, the slurry and the aggregate are in a good wrapped state, so that the agglomeration effect between the non-carbonized recycled fine aggregate mortar and the polyphenyl particles is relieved to a certain extent, and the distribution of the polyphenyl particles in the concrete is optimized. |[0103] Comparing the uniformity quantization index parameters of the polyphenyl granule concrete under the condition of 24h and 48h carbonization pretreatment, the absolute value of the uniformity performance index parameter of the 48h carbonization pretreatment group is generally lower than that of the 24h carbonization group, so that the optimal carbonization time is recommended to be 48h after the uniformity distribution factors of the polyphenyl granule are considered.|[0104] The beneficial effects are that: according to the technical scheme, the recycled aggregate performance is improved by carbonizing the recycled fine aggregate prepared from the waste concrete, a reference basis is provided for engineering application of the recycled fine aggregate subjected to subsequent carbonizing pretreatment, a large amount of waste concrete and polystyrene resources can be effectively recycled, natural sand and stone resources are saved, environmental protection is facilitated, solid waste of the building is reasonably utilized and carbon is stored, and the novel direction of green, low-carbon and energy-saving building development is met.|[0105] Finally, it should be noted that the above description is only a preferred embodiment of the present invention, and that many similar changes can be made by those skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims. (CN116854421)|TECHNICAL FIELD|[0001] The invention relates to the field of building materials, in particular to recycling of building waste.|BACKGROUND ART|[0002] With the promotion of new construction, demolition and reconstruction projects of buildings generated by urban construction and related production activities, a large amount of building wastes are generated, and the amount of waste concrete is increased gradually, and the annual growth speed is 5% -10%. The construction wastes cannot be recovered and cleared in time, so that the construction wastes cause a certain harm to the environment and limit the development speed of cities. With the continuous development of natural resources and the increase of the quantity of wastes, the sustainable utilization and management of the construction wastes have profound significance for the green development of the future construction industry.|[0003] The construction waste mainly comprises waste concrete, wherein the concrete comprises natural river sand, broken stone, cement, cementing material and various additives. After the discarded concrete is crushed, recycled concrete coarse aggregate (RCA), recycled concrete fine aggregate (RFA) and recycled micro powder (RCP) with the particle size meeting the relevant specifications can be obtained. The recycled aggregate mainly comprises 65-70% of natural aggregate and 30-35% of adhesive mortar by volume, and compared with the natural aggregate, most recycled aggregate has smaller density, more surface edges and corners and larger roughness. Meanwhile, due to the complex interface transition condition of the recycled aggregate, more or less cement mortar components exist on the crushed aggregate, and certain cracks can be generated on the aggregate in the mechanical treatment process, so that the physical properties of the recycled aggregate are weaker than those of the natural aggregate, and the recycled aggregate has higher porosity, water absorption and crushing indexes, thereby limiting the application of the recycled concrete as a bearing structure. The development of recycled concrete in the future will thus be mainly in terms of non-load-bearing structures. |[0004] Polystyrene particles (Expanded Polystyrene, EPS) are produced and used in large quantities as a high molecular petroleum compound material, and the polystyrene particles have the characteristics of light weight, heat preservation, heat insulation, sound insulation, moisture resistance and the like as a light foam wallboard material, and are widely applied as non-bearing structures in assembled buildings.|[0005] Therefore, the recycled concrete is expected to have a certain application prospect in the field of polystyrene particle wallboards.|DISCLOSURE|Disclosure of Invention|[0006] The invention adopts the method that the recycled fine aggregate is carbonized and modified and then is combined with the polystyrene particle material to prepare the carbonized recycled fine aggregate polystyrene concrete meeting the requirements of relevant standards, expands a new way of recycling and industrialization application of solid waste of buildings and popularizes the application of the recycled fine aggregate in engineering practice.|[0007] The main technical scheme adopted by the invention is as follows:|[0008] a method for preparing polyphenyl granule concrete by using carbonized regenerated fine aggregate is characterized by comprising the following steps:|[0009] step one, preparing recycled fine aggregate;|[0010] crushing the waste concrete blocks to obtain recycled fine aggregate;|[0011] firstly, stripping steel bars from waste concrete to obtain waste concrete blocks, primarily crushing to obtain 25-50mm recycled coarse aggregate, crushing by a jaw crusher, and screening by a vibrating screen to obtain recycled fine aggregate; |[0012] Step two, putting the regenerated fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; CO is introduced again 2 The pressure in the carbonization furnace is 0.1-0.4MPa, and carbonization is carried out for 12-48 hours to obtain carbonized fine aggregate;|[0013] step three, 600:240-360:120-240: and mixing cement, river sand, carbonized fine aggregate and EPS particles uniformly in a mass ratio of 7.5, and adding water according to a water-cement ratio of 0.46, and mixing uniformly.|DRAWINGS DESCRIPTION|[0014] FIG. 1 is a schematic view showing the structure of a carbonization furnace in example 2;|[0015] FIG. 2 is a top view of FIG. 1;|[0016] fig. 3 is a schematic view of the structure of the support plate 32;|[0017] FIG. 4 is a graph showing the effect of carbonization time-pressure on apparent density of aggregate corresponding to example 3;|[0018] FIG. 5 is a graph showing the effect of carbonization time-pressure on bulk density of aggregate corresponding to example 3;|[0019] FIG. 6 is a graph showing the effect of carbonization time-pressure on the close packing density of aggregates corresponding to example 3;|[0020] FIG. 7 is a graph showing the effect of carbonization time-pressure on aggregate saturation and dry water absorption for example 3;|[0021] FIG. 8 is a graph showing the influence of carbonization time-pressure on aggregate crushing index corresponding to example 3;|[0022] FIG. 9 is a graph showing the effect of carbonization time-pressure on aggregate pH corresponding to example 3;|[0023] FIG. 10 is a microscopic morphology of the non-carbonized recycled fine aggregate corresponding to example 3; |[0024] FIG. 11 is a graph of the microtopography of the carbonized aggregate corresponding to example 3;|[0025] FIG. 12 is an XRD diffraction pattern of carbonized aggregates at the same carbonization pressure and at different carbonization times corresponding to example 3;|[0026] FIG. 13 is an XRD diffraction pattern of carbonized aggregates at different carbonization pressures at the same carbonization time corresponding to example 3;|[0027] FIG. 14 is a graph of TG curve corresponding to example 3;|[0028] FIG. 15 is a graph of the corresponding DTG of example 3;|[0029] FIG. 16 is a plot of dry concrete density versus substitution for example 4;|[0030] FIG. 17 is a graph showing the water absorption of concrete under different carbonization conditions-substitution rate according to example 4|[0031] FIG. 18 is a concrete slump-displacement ratio bar chart corresponding to example 4;|[0032] FIG. 19 is a bar graph of compressive strength corresponding to example 4;|[0033] FIG. 20 is a bar graph of the split tensile strength corresponding to example 4.|INVENTION MODE|Detailed Description|[0034] The invention is further described below with reference to examples and figures.|[0035] Example 1:|[0036] the preparation process of polyphenyl granule concrete with carbonized regenerated fine aggregate includes the following steps:|[0037] step one, preparing recycled fine aggregate;|[0038] the test is selected from column and beam structural members of civil buildings in a brick-concrete structure, firstly, stripping reinforcing steel bars from waste concrete, primarily crushing the waste concrete by manpower or a machine to obtain regenerated coarse aggregate with the diameter of 25-50mm, then crushing the waste concrete by a jaw crusher, removing impurity components such as wood dust, iron wires and the like, and screening the waste concrete by a vibration screening machine to obtain regenerated fine aggregates with different particle diameters; |[0039] Step two, putting the regenerated fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; CO is introduced again 2 The pressure in the carbonization furnace is 0.1-0.4MPa, and carbonization is carried out for 12-48 hours to obtain carbonized fine aggregate;|[0040] for carbonization reaction of the aggregate, the small water content of the aggregate can lead to the incapability of timely dissolving carbon dioxide gas to participate in carbonation reaction, the large water content can lead to the aggregation phenomenon of water on the surface of the aggregate, and a large amount of calcium ions overflow the outer surface of the aggregate to not timely participate in carbonation reaction to influence the porosity of the aggregate, so that the proper water content of the aggregate is beneficial to the carbonization reaction.|[0041] Therefore, before carbonization, the recycled fine aggregate is preferably placed in an indoor environment at a temperature of 23 ℃ and a humidity of 45 to 55% for 7 days, and then placed in a carbonization furnace to be carbonized.|[0042] In a further preferred embodiment, in the second step, CO is introduced into the carbonization furnace 2 Until the pressure is 0.4MPa, the carbonization time is 48h.|[0043] Step three, 600:240-360:120-240: and mixing cement, river sand, carbonized fine aggregate and EPS particles uniformly in a mass ratio of 7.5, and adding water according to a water-cement ratio of 0.46, and mixing uniformly. |[0044] Example 2:|[0045] as shown in fig. 1, 2 and 3, the carbonization furnace comprises a tank body 1 and a tank cover 2 which is buckled on the tank body 1 in a sealing way, wherein the tank body 1 and the tank cover 2 are respectively provided with flanges which are matched with each other, and holes for connecting bolts are arranged on the flanges; at least three support legs 4 are arranged on the outer wall of the tank body 1. The support legs 4 overhead the tank body 1;|[0046] the bottom of the inner wall of the tank body 1 is an arc-shaped surface, the concave surface of the arc-shaped surface faces upwards, and the bottom of the tank body 1 is connected with a drain pipe 11 and CO 2 An air inlet pipe 12, said CO 2 The air inlet pipe 12 is vertically arranged, and the CO 2 The upper part of the air inlet pipe 12 extends into the tank body 1, and the CO 2 The upper end port of the air inlet pipe 12 is closed, and the CO is formed by 2 A lateral air inlet is arranged on the upper pipe wall of the air inlet pipe 12, and a negative pressure suction pipe 13 is connected to the upper part of the tank body 1; a drain valve is arranged on the drain pipe 11, and the CO is arranged on the drain pipe 2 The air inlet pipe 12 is provided with a pressure reducing valve;|[0047] the sewage drain pipe 11 is vertically arranged, the upper end of the sewage drain pipe 11 is connected with the lowest part of the arc-shaped surface, and the pipe orifice at the upper end of the sewage drain pipe 11 is communicated with the tank body 1; a pipe orifice blocking cover 14 is arranged in the tank body 1 corresponding to the upper end of the sewage drain pipe 11, the pipe orifice blocking cover 14 is buckled at the bottom of the tank body 1, the edge of the pipe orifice blocking cover 14 is fixedly connected with the inner wall of the tank body 1, and a plurality of small holes are formed in the pipe orifice blocking cover 14; |[0048] The tank cover 2 is provided with a thermometer 21, a safety valve 22 and an emptying pipe 23, and the emptying pipe 23 is provided with a pressure gauge.|[0049] A plurality of supporting tray components are vertically distributed in the tank body 1; the support tray assembly comprises at least three support blocks 31 and one support disc 32, wherein the support blocks 31 are fixed on the inner wall of the tank body 1, the support discs 32 are tiled in the tank body 1, the edges of the support discs 32 are lapped on the corresponding support blocks 31, and the edges of the support discs 32 are provided with yielding notches which correspond to the support blocks 31 one by one;|[0050] the support plate 32 may be of a fine mesh structure so that recycled fine aggregate is directly stacked thereon; the support plate 32 may have a coarse mesh structure, and the regenerated fine aggregate may be contained in a net bag and placed on the support plate 32.|[0051] Example 3:|[0052] selecting the same batch of recycled fine aggregate, randomly dividing the recycled fine aggregate into a plurality of parts, and carbonizing the recycled fine aggregate according to the parameter configuration of the following table 1:|[0053] TABLE 1 carbonization parameters of recycled fine aggregate|[0054] |[0055] According to the standard GB/T14684-2011, the aggregate density (including apparent density, loose bulk density and close bulk density), saturated surface dry water absorption, crushing index and pH of each group of carbonized fine aggregates are measured and compared with those of the original non-carbonized regenerated fine aggregates, and the results are shown in figures 4-9; |[0056] As can be seen from fig. 4, 5, 6: the density of the recycled fine aggregate can be increased by carbonization treatment. Compared with the regenerated fine aggregate which is not subjected to carbonization pretreatment, the carbonization pressure is increased from 0.1MPa to 0.4MPa under the same carbonization time treatment condition, and the apparent density is improved. The apparent density of the aggregate after 24 hours of treatment under the pressure of 0.1MPa is less than 0.2MPa and 0.4MPa, which is probably caused byUnder the condition of low pressure of 0.1MPa, calcium carbonate and other carbonization reaction products generated by the reaction of carbon dioxide with moisture, calcium hydroxide and other substances in the pores on the surface of the aggregate block the subsequent gas from entering the aggregate, so that the carbonization reaction degree of the subsequent aggregate is reduced, and the apparent density improvement effect of the aggregate under the carbonization condition is not good. With the increase of carbonization pressure from 0.1MPa to 0.2MPa and 0.4MPa, the apparent density can be increased by 27.51-94.13kg/m 3 . Has optimal carbonization effect under the condition of 0.4MPa, and has the maximum apparent density of 2650.42kg/m 3 。|[0057] Compared with the regenerated fine aggregate which is not subjected to carbonization pretreatment, under the same carbonization pressure treatment condition, the carbonization time is increased from 12h to 24h and 48h, and the apparent density is increased by 8.62-127.50kg/m 3 . Has the maximum improving effect under the condition of 48 hours, and the maximum apparent density is 2683.79kg/m 3 。|[0058] For loose bulk density, the influence of different carbonization pressures is small, and the bulk density after pretreatment for 24 hours under the pressure of 0.4MPa is only increased by 14.94kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The maximum bulk density after pretreatment under the conditions of 0.4MPa pressure and different carbonization times is only increased by 17.44kg/m 3 . For the compact bulk density, the apparent density can be increased by 76.1-114.56kg/m with increasing carbonization pressure from 0.1MPa to 0.2MPa and 0.4MPa 3 Compared with the recycled fine aggregate which is not subjected to carbonization pretreatment, the recycled fine aggregate is improved by 5.73 percent, 6.37 percent and 8.63 percent respectively, and the bulk density under the carbonization treatment condition of 0.4MPa-24h is the maximum and is 1442.13kg/m 3 . As the carbonization time increases from 12h to 24h and 48h, the close packing density can increase from 94.63 kg/m to 138.00kg/m 3 Compared with the recycled fine aggregate which is not subjected to carbonization pretreatment, the recycled fine aggregate is improved by 7.13 percent, 8.63 percent and 10.39 percent respectively, and the bulk density under the carbonization treatment condition of 0.4MPa to 48h is the maximum and is 1465.57kg/m 3 . The carbonization reaction generates calcium carbonate and other carbonization reaction products, so that the surface pores of the aggregate are filled and the aggregate is densified, and the mass fraction of the regenerated fine aggregate is larger under the condition of the same volume unit. Has similar conclusion with apparent density as carbonization The increase in the number of the elements increases the effect of carbonization on improving the bulk density of the recycled fine aggregate.|[0059] As can be seen from fig. 7: under the same carbonization time condition, the water absorption of the recycled fine aggregate shows a decreasing trend along with the increase of carbonization pressure, the carbonization pressure is increased from 0.1MPa to 0.2MPa and 0.4MPa, the water absorption of the recycled fine aggregate is respectively decreased by 16.97%, 24.51% and 29.31%, wherein the carbonization pressure with the best water absorption improvement effect on the recycled fine aggregate is 0.4MPa, and the water absorption of the aggregate is 7.50%. Under the same carbonization pressure, the water absorption of the recycled fine aggregate shows a decreasing trend along with the increase of the carbonization time, the carbonization time is increased from 12h to 24h and 48h, the water absorption of the recycled fine aggregate is respectively decreased by 15.55%, 29.31% and 31.67%, wherein the carbonization time with the largest water absorption improvement effect on the recycled fine aggregate is 48h, and the water absorption of the aggregate is 7.25%. The best carbonization condition of the test has 31.67 percent of water absorption reduction effect on the recycled fine aggregate.|[0060] As can be seen from fig. 8: the crushing index value of the recycled fine aggregate subjected to carbonization pretreatment is smaller than that of the recycled fine aggregate not subjected to carbonization pretreatment. Under the same carbonization time condition, the crushing index value of the recycled aggregate shows a decreasing trend along with the increase of carbonization pressure. When the carbonization time is controlled to be 24 hours, the carbonization pressure is increased from 0.1MPa to 0.2MPa and 0.4MPa, the crushing index values are respectively reduced by 3.23%, 6.45% and 19.35% compared with the crushing index values of the recycled aggregate which is not subjected to carbonization pretreatment, and the minimum crushing index value of the recycled aggregate subjected to carbonization treatment under the condition of 24 hours to 0.4MPa is 25%. Under the same carbonization pressure, the crushing index value of the recycled aggregate shows a decreasing trend with the increase of carbonization time. When the carbonization pressure is controlled to be 0.4MPa, after the carbonization time is increased from 12h to 24h and 48h, the crushing index values are respectively reduced by 9.68%, 19.35% and 25.81%, and the minimum crushing index value of the recycled aggregate subjected to carbonization treatment under the condition of 48h-0.4MPa is 23%. The carbonization pretreatment can effectively reduce the crushing index of the recycled aggregate. The carbonization pretreatment has the improvement effect on the crushing index of the recycled aggregate, mainly calcium carbonate crystals and other carbonization reaction products are produced through carbonation reaction, so that the surface micro-pore structure of the fine aggregate is filled, the strength grade of the aggregate is improved to a certain extent, and compared with the recycled aggregate which is not subjected to carbonization treatment, the recycled aggregate has a larger strength value, and the crushing index value is reduced. |[0061] As can be seen from fig. 9: under the same carbonization time conditions, it was found that the water absorption of the recycled fine aggregate showed a decreasing trend with increasing carbonization pressure. After the carbonization pressure is increased from 0.1MPa to 0.2MPa and 0.4MPa, the pH value of the recycled fine aggregate is respectively reduced by 24.75%, 27.68% and 28.52%, wherein the carbonization pressure with the best effect on improving the pH value of the recycled fine aggregate is 0.4MPa, and the pH value of the aggregate is 8.52. Under the same carbonization pressure, the pH value of the recycled fine aggregate was found to show a decreasing trend with increasing carbonization time. After the carbonization time is increased from 12h to 24h and 48h, the pH value of the recycled fine aggregate is respectively reduced by 24.66%, 28.52% and 28.86%, wherein the carbonization time with the best effect on improving the pH value of the recycled fine aggregate is 48h, and the pH value of the aggregate is 8.48.|[0062] The microscopic morphology of the surface of the regenerated fine aggregate and the carbonized aggregate is observed by a scanning electron microscope, and the results are shown in fig. 10 and 11 respectively.|[0063] As shown in fig. 10, the mortar component structure on the surface of the recycled fine aggregate which is not subjected to carbonization pretreatment is observed to be loose, a more obvious wide gap exists, and the interface transition zone of the recycled aggregate which is subjected to carbonization pretreatment in fig. 11 is observed to be more compact. The uncarbonized cement mortar has a loose and porous structure, and a large amount of white substances are distributed on the surface. The surface of carbonized cement slurry is found to contain a large amount of white granular matters agglomerated, the overall structure is remarkably tighter than that of the uncarbonated slurry, the pore structure is remarkably reduced, and a plurality of larger pores are gradually filled with matters generated by carbonization reaction to become smaller pore structures. This is mainly due to: on one hand, carbon dioxide enters the surface pores of the recycled aggregate and is dissolved in water, and then the carbon dioxide and calcium hydroxide in mortar generate carbonization reaction, so that carbonization reaction products such as calcium carbonate, silica gel and the like are filled in the surface pore structures of the recycled fine aggregate in microcracks, and the interface structure of the recycled fine aggregate is densified, so that the physical property of the recycled fine aggregate is improved. Meanwhile, a certain amount of needle-shaped ettringite crystals and C-S-H cementing materials are mutually interwoven in the mortar, but the mortar has more pore structures and larger gaps exist in an interface transition zone. On the other hand, certain regenerated micro powder exists on the surface of the regenerated fine aggregate, and the regenerated micro powder not only can play a role in filling gaps in the hydration process, but also can play a certain role in pozzolanic effect, so that more hydration products are generated in the interface transition zone, and the interface transition zone is improved to a certain extent. |[0064] The diffraction patterns of carbonized aggregates under the conditions of increasing carbonization time from 12h to 24h and 48h under the same carbonization pressure of 0.4MPa are respectively measured by adopting an XRD diffractometer, and the result is shown in figure 12;|[0065] under the same carbonization time condition of 24 hours, the diffraction patterns of carbonized aggregate when the carbonization pressure is increased from 0.1MPa to 0.2MPa and 0.4MPa are shown in the result of FIG. 13;|[0066] fig. 12 and 13 reflect the variation of diffraction peak intensity for recycled fine aggregates under different carbonization conditions. It can be seen that: after carbonization treatment, the diffraction peak intensity of calcium hydroxide and ettringite is obviously reduced, and the diffraction peak intensity of calcium carbonate is obviously increased.|[0067] Under the same carbonization pressure of 0.4MPa, the carbonization time is increased from 12h to 24h and 48h, and the intensity of the calcium carbonate diffraction peak is slightly increased but not obvious. However, when the pressure was increased from 0.1MPa to 0.2MPa or 0.4MPa with respect to the fixed 24-hour period, the diffraction peak was observed to be increased.|[0068] The TG curve and DTG curve under different carbonization conditions were measured, and the results are shown in fig. 14 and 15, respectively, and it can be seen from fig. 14 and 15: the first peak value change interval is 5-200 ℃, and the contrast shows that the mass loss difference in the range is more obvious, the quality change of untreated recycled aggregate is 7.43%, and the mass loss after carbonization treatment is only 1.98%. Mainly caused by the water decomposition of the bound water in hydration products such as calcium aluminate hydrate, AFt, C-S-H and the like which are contained in a certain amount in the raw aggregate. The second peak change lies in the range of 350-550 c, which is primarily the decomposition of the calcium hydroxide product. The obvious difference of the change condition of calcium hydroxide substances before and after carbonization is observed, which is mainly caused by the consumption of calcium hydroxide in the aggregate by carbonization reaction, and the quality loss of the aggregate after carbonization treatment is only 0.91 percent at most. The third peak change is in the range of 550-800 ℃, and the mass change degree is found to be more different, especially the mass loss of aggregate before and after carbonization. With increasing carbonization time, the mass loss was 39.69%, 44.92% and 48.67% in order; as the carbonization pressure increases, the mass loss is 39.17%, 39.87% and 44.92% in sequence; the quality loss of the regenerated fine aggregate which is not subjected to carbonization pretreatment is only 10.27%, and the carbonization treatment remarkably changes the quality change condition within the range of 550-800 ℃. The loss of quality may be due to the formation of calcium carbonate species of varying degrees of crystallization. The loss of calcium carbonate crystal decomposition in the range of 550 to 700 ℃ is considered to be poor in crystallization, and the mass change caused by calcium carbonate decomposition in the range of 700 to 800 ℃ is mainly good in crystallization. The conclusion is similar to XRD test results, and indicates that under the condition of a certain carbonization pressure, the carbonization reaction product generated by early carbonization reaction can effectively improve the pore structure of the surface of the aggregate, reduce the water absorption and enhance the performance of the aggregate. On the other hand, however, the calcium carbonate formed by the method and the corresponding carbonization reaction products are densified on the surface of the aggregate, and the carbon dioxide gas is prevented from entering and participating in the subsequent reaction, so that the difference of mass loss is not significant as carbonization time is increased in the figure. |[0069] And (3) carbonization mechanism analysis of the recycled fine aggregate: when carbonization reaction occurs, carbon dioxide gas firstly enters the surface and the inside of the aggregate, and is dissolved in the water of the aggregate to form carbonic acid. As the carbonation reaction proceeds, the pH of the solution in the original pores of the aggregate changes and becomes neutral. The ettringite (AFt), monosulfate (AFm), calcium hydroxide and other related substances in the raw mortar can be subjected to carbonization reaction. At ph=11.6, AFm begins to decompose to form alumina and AFt; at ph=10.6, AFt begins to decompose to form sulfate and hydroxide ions, providing a starting material for subsequent carbonization reactions. The carbonic acid and the calcium hydroxide in the mortar of the raw aggregate are subjected to carbonation reaction to generate calcium carbonate crystals, the calcium carbonate generated by the reaction exists in three forms of aragonite, vaterite and calcite, and the calcium carbonate is finally converted into calcite with good crystallization and exists stably. The C-S-H and other carbonizable substances also react with carbon dioxide to generate a certain content of calcium carbonate and gelled substances, and the gelled substances and calcium carbonate crystals generated by calcium hydroxide are clustered together and grow into blocks and adhere to the outer surface of the aggregate and the interface transition zone, so that the density of the aggregate is increased, and the water absorption rate of the aggregate is reduced. The carbonization mechanism can obviously improve the apparent density of the aggregate in early stage, and reduce the water absorption rate by 15.55% -31.67%; reducing the crushing index by 3.23-25.81%; the pH value is reduced by 24.66% -28.86%. However, when the carbonization condition is further changed, the carbonization time is increased, and the carbonization pressure is increased, it is found that the carbonization gain effect is gradually decreased. The early carbonization gain is mainly used for enabling generated carbonization reaction products to be attached to the surface of the aggregate and forming a relatively dense film in an interface transition zone, so that the subsequent carbonization reaction is prevented from being generated when carbon dioxide gas enters into gaps of the aggregate. |[0070] Example 4:|[0071] based on each carbonized aggregate (C1T 24, C2T24, C4T12, C4T24, C4T 48) obtained in example 3, polyphenyl granular concrete was prepared in the following proportions of table 2:|[0072] TABLE 2 polyphenyl granule concrete formulation Table (kg/m) 3 )|[0073] |[0074] In Table 2, the amount of river sand was 480kg/m based on the N group of non-recycled fine aggregate/carbonized aggregate 3 The method comprises the steps of carrying out a first treatment on the surface of the Replacing part/all river sand with recycled fine aggregate/carbonized aggregate according to different substitution rates (25%, 50%, 75%, 100%);|[0075] substitution rate= (amount of recycled fine aggregate/amount of carbonized aggregate)/480 x 100%.|[0076] According to GB/T50081-2019 Standard of method for testing physical and mechanical properties of common concrete, concrete with various proportions in Table 2 is used as a raw material, and a standard test piece of polystyrene particle recycled fine aggregate concrete with the dimensions of 100mm multiplied by 100mm is prepared by test design to test the mechanical properties of the concrete. Because the recycled fine aggregate has higher aggregate water absorption rate, saturated water absorption treatment is needed to avoid the influence of the local water-cement ratio difference of concrete caused by direct water addition when the concrete is prepared, and thus the concrete is needed to be prepared according to the preparation flow of the figure. Firstly, uniformly stirring natural aggregate and regenerated fine aggregate, putting 1/3 of water into the mixture to saturate the mixture, stirring the mixture for 2 minutes, putting cement and the rest 1/2 of water into the mixture to stir the mixture for 3 minutes, finally, adding the rest of water into the mixture to stir the mixture for 3 minutes, and uniformly putting EPS particles into the mixture to stir the mixture for 5 minutes after the cement is fully stirred. And then the uniformly mixed concrete material is layered and placed into a steel test die, and is uniformly distributed by adopting a manual insertion and tamping mode, and is put into the die, and then is subjected to film coating treatment in time, and is subjected to demoulding treatment after being cured for 24 hours in an environment with the relative humidity of more than 50 percent at 20+/-5 ℃, and the samples are separated from each other by 10-20mm and are placed into a standard constant temperature and humidity curing box with the relative humidity of more than 95 percent at 20+/-2 ℃ for standard curing. And (5) after 28d standard curing, taking out in time, and putting into an infrared blast drying oven with the temperature of 105+/-5 ℃ for drying treatment, and keeping for later use. |[0077] The dry density of the concrete was tested with reference to specification GB/T50081-2019, the results being shown in FIG. 16;|[0078] as can be seen from fig. 16, as the substitution rate of recycled aggregate increases, the dry density of the recycled fine aggregate polyphenyl granule concrete decreases. When the substitution rate of the recycled fine aggregate is increased from 25% to 100%, the dry density thereof is increased from 1323.83g/cm 3 Reduced to 1311.37g/cm 3 The method comprises the steps of carrying out a first treatment on the surface of the When the C4T24 carbonized regenerated fine aggregate is adopted, the dry density of the concrete adopting the carbonized regenerated fine aggregate is from 1339.97g/cm 3 Reduced to 1318.10g/cm 3 . The carbonization pretreatment improves the dry density value of the concrete, but the improvement effect is not obvious, and the maximum dry density value of the concrete is improved by 1.22 percent only under the condition of 25 percent substitution rate. When the C4T48 carbonization is adopted to regenerate the fine aggregate, the dry density of the concrete is 1346.23g/cm 3 Reduced to 1320.86g/cm 3 The density increase was slightly higher than that of the C4T24 control, again increasing by a maximum of 1.69% at 25% substitution. Carbonization timeThe increase of the density of the concrete is achieved, the lifting effect is derived from carbonization pretreatment, so that the apparent density of the recycled fine aggregate is increased, and the surface of the carbonized recycled aggregate has more calcium carbonate crystals and carbonization reaction products in the same volume state, so that the mass fraction of the aggregate is increased, and the dry density value of the concrete is further improved. |[0079] The water absorption of concrete was tested with reference to specification GB/T50081-2019 and the results are shown in FIG. 17. The RCA in fig. 17 includes four sets of water absorption rates R25, R50, R75, R100 in table 2; C4T24 includes four sets of water absorption in table 2, C4T24R25, C4T24R50, C4T24R75, C4T24R 100; the C4T48 includes four sets of water absorption rates C4T48R25, C4T48R50, C4T48R75, C4T48R100 in Table 2. As can be seen from fig. 17, the water absorption of the recycled fine aggregate concrete without carbonization pretreatment is generally higher than that of the carbonized group. Wherein the water absorption of the concrete after 24 hours carbonization pretreatment is reduced by 35.49%, 34.97%, 29.13% and 23.29% respectively compared with the non-carbonized control group, and the concrete has the minimum water absorption value of 10.99% when the fine aggregate substitution rate is 25%. As carbonization time increases from 24h to 48h, the concrete water absorption value shows a decreasing trend, but the change degree is not significant, and the water absorption value is respectively decreased by 5.88%, 4.00%, 4.33% and 5.65% under different substitution rate conditions relative to a 24h carbonization group. Due to the presence of the carbonization reaction inhibition, the water absorption rate increases with the increase of the carbonization time under the same carbonization conditions, but the improvement effect thereof is not significant.|[0080] Slump of concrete was tested with reference to specification GB/T50080-2002, the results being shown in FIG. 18; |[0081] According to the concrete slump test result shown in fig. 18, in the case where the cement ratio is the same, as the substitution rate of the recycled fine aggregate increases, the fluidity of the concrete decreases, and the slump decreases, wherein the slump is only 116mm under the substitution rate of 100% of the total recycled aggregate, and the slump is decreased by 38.95% compared with the natural control group. After carbonization pretreatment, the fluidity of the concrete is improved, and the slump of the concrete is improved by the carbonization pretreatment of the recycled fine aggregate. The improvement effect of the recycled fine aggregate under the carbonization treatment condition of C4T24 is smaller at the low substitution rate of 0-50%, which is 185mm and 180mm respectively; the improvement effect is obvious under the condition of 50-100% substitution rate, and the flowability under the condition of 75% and 100% regeneration fine aggregate substitution rate is 167mm and 149mm. Compared with a control group without carbonization treatment, the 100% of the fully regenerated carbonized regenerated fine aggregate concrete has 28.45% of improved performance.|[0082] The improvement effect of the recycled fine aggregate under the carbonization treatment condition of C4T48 is observed to be smaller at a low substitution rate of 25%, which is 187mm; the improvement effect is obvious under the condition of 50-100% substitution rate, and the flowability under the condition of 50%, 75% and 100% regeneration fine aggregate substitution rate is 184mm, 175mm and 156mm. Compared with a control group without carbonization treatment, the 50% of the fully regenerated carbonized regenerated fine aggregate concrete has the performance improved by 40.00%. |[0083] The working performance analysis of the regenerated fine aggregate control group treated under the same pressure condition and different carbonization time shows that the regenerated fine aggregate group carbonized for 48 hours has a larger slump value, and compared with the 24-hour carbonized group, the regenerated fine aggregate control group has different degrees of improvement of 1.08-4.79 percent under the condition of 25-100 percent substitution rate, and has larger flow performance under the condition of the same water cement ratio.|[0084] The recycled aggregate which is not carbonized is extremely easy to cause more edges and corners on the surface of the aggregate, microcracks and the existence of recycled micro powder, mud blocks and other substances in the crushing process, so that the water demand of the concrete is increased, and the free water in the concrete using the recycled fine aggregate is reduced under the condition of the same water-cement ratio, thereby reducing the flowability of the concrete. The improvement of the fluidity is mainly beneficial to the carbonization reaction, so that compact calcium carbonate crystal components can be formed on the surface of the aggregate to fill the pores, the water absorption rate of the recycled aggregate is reduced, more free water on the surface of the aggregate can exist in the concrete preparation process, and the fluidity of the mixture is greatly increased.|[0085] The concrete cubes were tested for compressive strength with reference to specification GB/T50081-2019, the results being shown in FIG. 19; |[0086] As can be seen in connection with fig. 19, the concrete using the recycled fine aggregate has lower overall strength than the control group using the natural river sand aggregate, which is mainly caused by the recycled fine aggregate attaching mortar and the self-void structure. The recycled fine aggregate contains a large amount of waste mortar, has lower strength, and generates a larger interface transition area when the recycled fine aggregate is combined with the new mortar to form concrete, so that the compressive strength of the concrete is lower than that of common concrete. Meanwhile, a large number of microcracks exist on the recycled fine aggregate after the recycled fine aggregate is treated in a mechanical crushing mode, and the compressive strength of the concrete is also adversely affected. In addition, the fact that the machine-made sand grading adopted by the recycled fine aggregate is different from the natural river sand to a certain extent is considered, and the components such as micro powder, mortar and the like in the recycled fine aggregate can absorb certain moisture in the concrete preparation process to cause local water-cement ratio change, so that the hydration of the cement is prevented from influencing the strength increase of the concrete.|[0087] The compressive strength of the concrete generally tends to decrease with increasing substitution rate of the recycled fine aggregate, wherein the compressive strength of the concrete using the recycled fine aggregate is lower than that of the concrete of the common control group using the natural aggregate. Meanwhile, the concrete adopting the carbonized regenerated fine aggregate is generally higher than the concrete control group which is not carbonized, which benefits from accelerating carbonization to generate a large amount of calcium carbonate crystals and other reaction products, and the concrete has a strengthening effect on the whole of the original regenerated aggregate and the attached mortar. |[0088] The recycled fine aggregate concrete has a similar strength development rule with the common concrete, the compressive strength of the recycled fine aggregate concrete shows a growth trend along with the increase of curing time, and the early strength of the concrete is obviously increased in 3-7d compared with 7-28 d. The strength of the concrete which adopts the recycled fine aggregate without carbonization pretreatment is increased by 4.88% -9.15% in the early stage of 3-7d, wherein the strength is increased to the maximum of 9.15% when the substitution rate is 50%; the increase in strength was 3.46% -8.63% at early 7-28d, with a maximum increase in strength of 8.63% at a substitution rate of 50%. The carbonization pretreatment obviously improves the change condition of the growth, the strength of the concrete adopting the C4T24 carbonized regenerated fine aggregate can reach 7.36-13.16% in early 3-7d, wherein the strength can reach 13.16% at maximum when the substitution rate is 50%; the strength increase can reach 6.97% -11.74% in 7-28d, wherein the maximum strength increase can reach 11.74% under the condition of 50% substitution rate. The strength of the concrete adopting the C4T48 carbonized and regenerated fine aggregate can reach 11.00% -13.76% in early 3-7d, wherein the maximum strength increase can reach 13.16% when the substitution rate is 50%; the strength increase can reach 6.97% -11.74% in 7-28d, wherein the maximum strength increase can reach 11.74% under the condition of 50% substitution rate. |[0089] Comparing the recycled fine aggregate concrete which is not carbonized and pretreated in the same period with the recycled fine aggregate concrete which is carbonized and treated under different conditions, the method has the following advantages that: the concrete pretreated by C4T24 carbonization has the improvement effect of 0.38-2.68%, 2.74-5.88% and 5.33-7.49% of compressive strength respectively at 3d, 7d and 28d, and the maximum compressive strength value is 9.61MPa. The strength improvement effect of the C4T24 on concrete is mainly between 3 and 28 days, and the strength improvement effect of the C4T24 on 3 days is not remarkable. The compressive strength of the concrete pretreated by C4T48 carbonization is respectively improved by 1.25 to 8.89 percent, 6.52 to 13.49 percent and 5.45 to 9.62 percent at 3d, 7d and 28 d. The improvement effect is superior to that of a carbonization control group for 24 hours under the same carbonization pressure, wherein the strength increase under the condition of 50 percent substitution rate is 8.89 percent, 13.49 percent and 9.62 percent respectively, and the maximum compressive strength is 9.80MPa. It is therefore recommended that the optimum recycled fine aggregate substitution rate be 50%.|[0090] After carbonization treatment, the compressive strength of the concrete is obviously improved. The carbonization technology is beneficial to the improvement of the pore structure of the recycled fine aggregate by generating a large amount of calcium carbonate crystals in the recycled fine aggregate, so that the recycled fine aggregate is more densified. The carbonization reaction product and the hydration reaction product can effectively fill the interface transition area between the recycled aggregate and the new mortar, thereby improving the compressive strength of the concrete. However, the improvement and improvement effect of the carbonization time from 24h to 48h on the compressive strength of the concrete is not obvious, and the compressive strength of the 28d concrete is only improved by 0.11% -1.98% when the compressive strengths of two different carbonization conditions are compared. Under the same carbonization pressure conditions, the improvement of the compressive strength is not obvious as the carbonization time increases from 24h to 48 h. |[0091] This also explains from another aspect that the carbonization effect is affected by the carbonization time so that the carbonization effect does not show an increasing trend with time to some extent, the improvement effect thereof is affected by the improvement of early carbonization, so that the later carbonization time increases but the subsequent carbon dioxide cannot sufficiently enter the inside of the recycled aggregate to provide the carbonization reaction raw material so that the improvement effect gradually declines. The optimal carbonization time is therefore recommended to be 24h.|[0092] The concrete split tensile strength was tested according to GB/T50081-2019 and the results are shown in FIG. 20;|[0093] as shown in fig. 20, the concrete using recycled aggregate has significantly lower split tensile strength than concrete using natural river sand as fine aggregate. With the increase of the substitution rate of the recycled aggregate, the splitting tensile strength of the concrete gradually decreases, but the carbonization pretreatment improves the strength of the concrete. As the substitution rate increases, the split tensile strength of the recycled fine aggregate concrete is reduced by 9.40%, 16.98%, 23.23% and 32.45% respectively compared with the natural river sand concrete control; the concrete reduction levels using the carbonized recycled fine aggregate were 7.26%, 16.04%, 22.73% and 25.0%, respectively. The carbonization treatment improves the splitting tensile strength of the recycled concrete by 0.53-8.09%, wherein the improvement effect of the recycled concrete on 100% of the fully recycled fine aggregate concrete is optimal and reaches 8.09%. It is therefore recommended that the optimum recycled fine aggregate substitution rate be 25%. Mechanism analysis: the splitting tensile strength of the recycled fine aggregate concrete is lower than that of the natural fine aggregate concrete control group, and the splitting tensile strength of the recycled fine aggregate concrete subjected to carbonization pretreatment is higher than that of the recycled fine aggregate concrete control group which is not subjected to treatment. Wherein, the splitting tensile strength of the recycled concrete shows a decreasing trend along with the increase of the substitution rate of the aggregate and the carbonized aggregate. The recycled aggregate consists of cement mortar and natural aggregate, wherein the recycled mortar has a larger pore structure and a larger water absorption rate. Meanwhile, the recycled fine aggregate contains more recycled micro powder, mud blocks and other substances in the preparation process, so that the water absorption of the recycled fine aggregate is increased, the free water consumption participating in hydration reaction in the mixing process is reduced, cement is hindered from participating in hydration reaction, the bonding degree of cement mortar and aggregate is reduced, and the splitting tensile strength of concrete is further influenced. After the recycled fine aggregate subjected to carbonization pretreatment is adopted, the splitting tensile strength of the recycled fine aggregate is improved. The carbonization effect produces a large amount of calcium carbonate crystals and carbonized products on the surface and in the pores of the aggregate, reduces the water demand of the recycled fine aggregate in the mixing process, ensures that more free water can exist in the mixing process to fully carry out hydration reaction with cement, increases the bonding capability of cement paste and the aggregate, and achieves the aim of improving the splitting tensile strength of the concrete. |[0094] Example 5:|[0095] a uniformity test method of polyphenyl granule concrete comprises the following steps:|[0096] according to GB/T50081-2019 "standard for test method of physical and mechanical properties of ordinary concrete", cylindrical samples with a diameter of 150mm and a height of 300mm were prepared according to the method of example 1, using concrete of each proportion in Table 2 as a raw material. Because the recycled fine aggregate has higher aggregate water absorption rate, saturated water absorption treatment is needed to avoid the influence of the local water-cement ratio difference of concrete caused by direct water addition when the concrete is prepared, and thus the concrete is needed to be prepared according to the preparation flow of the figure. Firstly, uniformly stirring natural aggregate and regenerated fine aggregate, putting 1/3 of water into the mixture to saturate the mixture, stirring the mixture for 2 minutes, putting cement and the rest 1/2 of water into the mixture to stir the mixture for 3 minutes, finally, adding the rest of water into the mixture to stir the mixture for 3 minutes, and uniformly putting EPS particles into the mixture to stir the mixture for 5 minutes after the cement is fully stirred. And then the uniformly mixed concrete material is layered and placed into a steel test die, and is uniformly distributed by adopting a manual insertion and tamping mode, and is put into the die, and then is subjected to film coating treatment in time, and is subjected to demoulding treatment after being cured for 24 hours in an environment with the relative humidity of more than 50 percent at 20+/-5 ℃, and the samples are separated from each other by 10-20mm and are placed into a standard constant temperature and humidity curing box with the relative humidity of more than 95 percent at 20+/-2 ℃ for standard curing. After 28d standard maintenance, taking out in time, and putting into an infrared blast drying oven with the temperature of 105+/-5 ℃ for drying treatment, and keeping for later use; |[0097] Cutting the cylindrical sample into two parts along the axial section of the cylindrical sample, exposing the section of the cylindrical sample, and acquiring images of the section; manually cutting the acquired image, and reserving an effective part;|[0098] binary conversion is carried out on the cut image, the picture type is converted into 8-bit from RGB, and noise reduction treatment is carried out at the same time, so that an analysis image is obtained;|[0099] cutting the analysis Image into 5 parts along the average, and introducing Image J software to perform identification and segmentation treatment on the internal polyphenyl particles;|[0100] and extracting the number and position distribution related information parameters of the polyphenyl particles in the image through software analysis and calculation.|[0101] Through researches on the uniformity distribution situation of polyphenyl particles in concrete under the conditions of different carbonization times of 24 hours and 48 hours and different substitution rates of 25%, 50%, 75% and 100% of recycled fine aggregates, the particle quantity uniformity index parameter of polyphenyl particle concrete of the recycled fine aggregates is generally lower than that of a natural river sand control group, and the main reasons are high water absorbability, irregular morphology and edges of the recycled fine aggregates.|[0102] The carbonized aggregate treated by carbonization effectively improves the distribution of polyphenyl particles in concrete, and in carbonized aggregate polyphenyl particle concrete, along with the increase of the aggregate substitution rate, the absolute values of various uniformity index parameters of the concrete are in a decreasing trend. The carbonization treatment fills the pore structure on the surface of the aggregate, and reduces the water absorption rate of the aggregate. Under the same water-cement ratio condition, the slurry and the aggregate are in a good wrapped state, so that the agglomeration effect between the non-carbonized recycled fine aggregate mortar and the polyphenyl particles is relieved to a certain extent, and the distribution of the polyphenyl particles in the concrete is optimized. |[0103] Comparing the uniformity quantization index parameters of the polyphenyl granule concrete under the condition of 24h and 48h carbonization pretreatment, the absolute value of the uniformity performance index parameter of the 48h carbonization pretreatment group is generally lower than that of the 24h carbonization group, so that the optimal carbonization time is recommended to be 48h after the uniformity distribution factors of the polyphenyl granule are considered.|[0104] The beneficial effects are that: according to the technical scheme, the recycled aggregate performance is improved by carbonizing the recycled fine aggregate prepared from the waste concrete, a reference basis is provided for engineering application of the recycled fine aggregate subjected to subsequent carbonizing pretreatment, a large amount of waste concrete and polystyrene resources can be effectively recycled, natural sand and stone resources are saved, environmental protection is facilitated, solid waste of the building is reasonably utilized and carbon is stored, and the novel direction of green, low-carbon and energy-saving building development is met.|[0105] Finally, it should be noted that the above description is only a preferred embodiment of the present invention, and that many similar changes can be made by those skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims. Family Number|(106780457)|106780457|Abstract|(CN116854421 A)|The invention discloses a method for preparing polyphenyl granule concrete by utilizing carbonized recycled fine aggregate , which comprises the following steps : firstly , crushing waste concrete blocks to obtain recycled fine aggregate ; then putting the recycled fine aggregate into a carbonization furnace , and vacuumizing to - 0.1 MPa ; cO2 is introduced into the carbonization furnace until the pressure intensity is 0.1-0.4 MPa , carbonization is performed for 12-48 h , and carbonized fine aggregate is obtained ; and finally , uniformly mixing the cement , the river sand , the carbonized fine aggregate and the EPS particles according to a mass ratio of 600 : 240-360 : 120-240 : 7.5, adding water according to a water - cement ratio of 0.46, and uniformly mixing . The method has the remarkable effects that the performance of the recycled aggregate is improved by performing carbonization pretreatment on the recycled fine aggregate prepared from the waste concrete , a reference basis is provided for subsequent engineering application of the recycled fine aggregate subjected to carbonization pretreatment , a large amount of waste concrete and polystyrene resources can be effectively recycled , natural gravel resources are saved , and the economic benefit is increased . Environment protection is facilitated , building solid waste is reasonably utilized and subjected to carbon sequestration , and the new direction of green , low - carbon and energy - saving building development is met . |CPC codes|(CN116854421 A)|G01N - 015/00 |IPC codes|(CN116854421 A)|G01N - 015/00 | Materials, metallurgy|Measurement C04B-020/02/3|C04B-028/02|C04B-2201/20|C04B-2201/50|G01N-015/00|Y02W-030/91 (GR1) C04B-028/02[RK1]; C04B-014/06[RK2]; C04B-016/08[RK3]; C04B-020/02/3[RK4]|(GR2) C04B-020/02/3[RK1]; C04B-018/16[RK2] C04B-020/02/3|C04B-028/02|C04B-2201/20|C04B-2201/50|G01N-015/00|Y02W-030/91 C04B-020/02|C04B-028/02|G01N-015/00 C04B-020/02|C04B-028/02|G01N-015/00 CN119241159|CN118307986 CN119241159 112904317 WHO=Examiner SELF=N CAT=A|CN118307986 110548623 WHO=Examiner SELF=N CAT=A CN104045251|CN115205252|CN106277885|CN105174766|KR101391991|JP05330870 CN104045251 67468563 WHO=Examiner SELF=N CAT=Y CAT=X|CN115205252 102174432 WHO=Examiner SELF=N CAT=Y|CN106277885 75072551 WHO=Examiner SELF=N CAT=Y|CN105174766 71814418 WHO=Examiner SELF=N CAT=A|KR101391991 66381542 WHO=Examiner SELF=N CAT=A|JP05330870 28374647 WHO=Examiner SELF=N CAT=A 王洪镇等: &quot;《流态轻集料微孔混凝土技术》&quot;, 31 October 2013, 中国建材工业出版社, pages: 183 - 184 (Cat. A)|韩长菊等: &quot;《通用混凝土生产》&quot;, 31 January 2022, 中国建材工业出版社, pages: 63 (Cat. A) JP05330870; KR101391991; CN104045251; CN105174766; CN106277885; CN115205252 PENDING (CN116854421)|PENDING ALIVE (CN116854421)|ALIVE (CN116854421)|LEGAL DETAILS FOR CN116854421|Actual or expected expiration date=2043-06-27|Legal state=ALIVE|Status=PENDING|Event publication date=2023-06-27|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202310772521|Application date=2023-06-27|Standardized application number=2023CN-0772521|Event publication date=2023-10-10|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN116854421|Publication stage code=A|Publication date=2023-10-10|Standardized publication number=CN116854421|Event publication date=2023-10-10|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-10-27|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN116854421)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSYBNqDJ+FMd1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000069783014&ekey=2304&xpn=CN116854421&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=MsjgTkfC88kWO3ErPm6qwZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN116854421)|CN (CN116854421)|NAME=CHONGQING HEFENG ZHUJIAN TECHNOLOGY CO., LTD. , COUNTRY=CN (CN116854421)|NAME=YAO KUN;CHONGQING QIANSHI PATENT AGENCY (GENERAL PARTNERSHIP) , REG=50259 (CN116854421)|NAME=SU XIN|NAME=FENG CHUNLAN|NAME=YOU YARAN|NAME=FENG RENJIANG|NAME=OUYANG YUHUI|NAME=BU CHANGMING|NAME=ZHANG MINGTAO|NAME=SUN YI|NAME=SHI YANGXI|NAME=ZHANG XUETAO|NAME=TANG JING 0 1 Titre: (CN116854421)|Method for preparing polyphenyl granule concrete by utilizing carbonized recycled fine aggregate and uniformity testing method Résumé: (CN116854421)|The invention discloses a method for preparing polyphenyl granule concrete by utilizing carbonized recycled fine aggregate, which comprises the following steps: firstly, crushing waste concrete blocks to obtain recycled fine aggregate; then putting the recycled fine aggregate into a carbonization furnace, and vacuumizing to-0.1 MPa; cO2 is introduced into the carbonization furnace until the pressure intensity is 0.1-0.4 MPa, carbonization is performed for 12-48 h, and carbonized fine aggregate is obtained; and finally, uniformly mixing the cement, the river sand, the carbonized fine aggregate and the EPS particles according to a mass ratio of 600: 240-360: 120-240: 7.5, adding water according to a water-cement ratio of 0.46, and uniformly mixing. The method has the remarkable effects that the performance of the recycled aggregate is improved by performing carbonization pretreatment on the recycled fine aggregate prepared from the waste concrete, a reference basis is provided for subsequent engineering application of the recycled fine aggregate subjected to carbonization pretreatment, a large amount of waste concrete and polystyrene resources can be effectively recycled, natural gravel resources are saved, and the economic benefit is increased. Environment protection is facilitated, building solid waste is reasonably utilized and subjected to carbon sequestration, and the new direction of green, low-carbon and energy-saving building development is met. 67 Abstract gpt-4o-mini no The article focuses on a method for preparing concrete using carbonized recycled aggregates, which does not involve the accelerated weathering of minerals for CO₂ capture.
68 CN201910425889 CN201910425889 CN110451510 86637865 CN110451510 A 2019-11-15 [CN110451510] 2019-05-21 2019-05-21 2019-11-15 (CN110451510)|2021-08-17 (CN110451510)|Silicon carbide surface treatment method (CN110451510)|The invention discloses a silicon carbide surface treatment method which comprises the following steps: I, crushing silicon carbide granules, and screening silicon carbide powder of which the particlesize is 5-10[mu] m; II, calcining the silicon carbide powder in a muffle furnace of 700-800 DEG C so as to remove free carbon on the surface of the silicon carbide powder; III, performing acid pickling and alkali wash on the silicon carbide powder after carbon removal so as to purify the silicon carbide powder after carbon removal; and IV, respectively performing dispersion pulping, physical dispersion, precipitate separation and drying on the silicon carbide powder after purification, so as to obtain silicon carbide micro powder after surface treatment. By adopting the silicon carbide surface treatment method disclosed by the invention, impurities on the surface of silicon carbide can be specifically removed, the dispersibility of the silicon carbide micro powder can be improved, in addition, the cost is low, and the energy consumption is low. HUNAN TAIZI NEW MATERIAL TECHNOLOGY (CN110451510)|HUNAN TAIZI NEW MATERIAL TECHNOLOGY CO., LTD. ([CN]) LIU JUN|LIU ZHENHUA|ZHANG HAI (CN110451510)|LIU JUN|LIU ZHENHUA|ZHANG HAI (CN110451510)|WANG XINAI;BEIJING SKYINTEL PATENT AGENCY|Reg. Nb: 11638 (CN110451510)|The silicon carbide surface treatment method provided by the invention has the advantages of simple process, low cost and low energy consumption, and improves the dispersibility of the silicon carbide micro powder.|In the above process, although the separation of silicon carbide micro powder with different particle sizes can be theoretically realized, in practice, complete separation of some particles with very different particle sizes is difficult to realize, for example, a large amount of nano silicon carbide particles (the main component is SiO) are adhered to the surface of micron silicon carbide micro powder particles2And low-purity silicon carbide), while the presence of the nano-scale silicon carbide particles can reduce the purity of the silicon carbide micro powder, affect the fluidity, the dispersibility and the bulk density of the micro powder, and preferentially react with a sintering aid, so that the forming performance and the sintering performance of the silicon carbide micro powder are poor, and the performance of a final silicon carbide fine ceramic product is reduced.| (CN110451510)|1. A silicon carbide surface treatment method is characterized by comprising the following steps:step one, crushing silicon carbide particles and screening silicon carbide powder with the particle size of 5-10 microns;placing the silicon carbide powder in a muffle furnace at the temperature of 700-800 ℃ for calcining to remove free carbon on the surface of the silicon carbide powder;step three, carrying out acid washing and alkali washing on the silicon carbide powder subjected to carbon removal so as to purify the silicon carbide powder subjected to carbon removal;step four, using organic silicon and organic fluorine as surfactants, using ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, then adding the silicon carbide powder obtained in the step three and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 3-5 hours for reaction at the temperature of 45-58 ℃ and the rotation speed of 500 plus materials per minute;and step five, respectively dispersing and slurrying the silicon carbide powder obtained by the surface treatment reaction in the step four, physically dispersing, precipitating, separating and drying to obtain the silicon carbide micro powder after surface treatment.| (CN110451510)|An object of the present invention is to solve at least the above problems and to provide at least the advantages described later. The invention also aims to provide a silicon carbide surface treatment method which can specifically remove impurities on the silicon carbide surface, improve the dispersibility of the silicon carbide micro powder and has low cost and low energy consumption. In order to achieve the aim, the invention discloses a silicon carbide surface treatment method, which comprises the following steps:|The invention discloses a silicon carbide surface treatment method, which comprises the following steps: step one, crushing silicon carbide particles and screening silicon carbide powder with the particle size of 5-10 microns; placing the silicon carbide powder in a muffle furnace at the temperature of 700-800 ℃ for calcining to remove free carbon on the surface of the silicon carbide powder; step three, carrying out acid washing and alkali washing on the silicon carbide powder subjected to carbon removal so as to purify the silicon carbide powder subjected to carbon removal; and step four, respectively dispersing and slurrying the purified silicon carbide powder, physically dispersing, precipitating and separating, and drying to obtain the surface-treated silicon carbide micro powder.|The invention relates to the technical field of silicon carbide micro powder, in particular to a silicon carbide surface treatment method.| (CN110451510)|SILICON CARBIDE(100,152)|SILICON CARBIDE POWDER(100,89)|SURFACE TREATMENT(100,48)|SILICON CARBIDE SURFACE TREATMENT(100,15)|ALKALI WASHING(62,15)|CRUSHING SILICON CARBIDE(53,8)|CONCENTRATED DEBACTEROL(52,14)|ORGANIC FLUORINE(51,21)|ACIDIC WASH(46,15)|REACTION KETTLE(46,14)|BETA SODIUM SULFONATE FORMALDEHYDE(42,14)|REMOVING CARBON(41,16)|SILICON CARBIDE MICRO POWDER(39,12)|MUFFLE FURNACE(37,8)|ORGANIC SILICON(35,19)|DISPERSANT(33,14)|SILICON CARBIDE SLURRY(33,14)|DISPERSIBILITY(30,1)|ALKALINE WASH MEDIUM(26,2)|MICRO POWDER(25,15)|CONDENSATE(25,14)|PICKLING MEDIUM(25,7)|ALKALI CLEANING(24,7)|SURFACTANT(23,7)|ORGANOSILICON(23,2)|STEP FOUR(22,4)|CLEANING FREQUENCY(21,12)|ALKALINE WASH TEMPERATURE(20,2)|CALCINING TEMPERATURE(20,2)|PICKLING TEMPERATURE(19,7)|IMPURITY(19,2)|ACIDIC CLEANING(18,7)|HYDROGEN FLUORIDE(17,14)|DEIONIZED WATER(16,35)|STEP THREE(15,5)|ENERGY CONSUMPTION(14,1)|WEIGHT RATIO(13,21)|FLUOROCARBOXYLIC ACID(13,7)|SILANE(13,7)|PLUS MATERIAL(13,2)|VOLUME RATIO(12,21)|SURFACE TREATMENT REACTION KETTLE(12,14)|PARTICLE SIZE(12,8)|ALKALI WASHING MEDIUM(12,5)|DECARBONIZATION(12,5)|PRECIPITATION SEPARATION(12,5)|SODIUM HYDROXIDE(11,7)|CLEANING TIME(10,16)|CRUSHING(10,6)|ALKALI WASHING TEMPERATURE(9,5)|ROTATION SPEED(9,2)|CALCINATION(8,4)|PRECISION CLASSIFICATION(8,1)|ALKALI WASHING(7,7)|ALKALINE WASHING TIME(7,2)|SILICON CARBIDE FINE CERAMIC(7,2)|PICKLING TIME(6,7)|POLYCARBOXYLIC ACID TYPE SURFACTANT(6,7)|PURIFICATION(6,6)|PICKLING(6,5)|ROTATING SPEED(6,5)|ROOM TEMPERATURE(5,7)|REACTING SURFACE TREATMENT(5,2)|DIFFICULT AGGLOMERATION(5,1)| (CN110451510)|1. A silicon carbide surface treatment method is characterized by comprising the following steps:|step one, crushing silicon carbide particles and screening silicon carbide powder with the particle size of 5-10 microns;|placing the silicon carbide powder in a muffle furnace at the temperature of 700-800 ℃ for calcining to remove free carbon on the surface of the silicon carbide powder;|step three, carrying out acid washing and alkali washing on the silicon carbide powder subjected to carbon removal so as to purify the silicon carbide powder subjected to carbon removal;|step four, using organic silicon and organic fluorine as surfactants, using ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, then adding the silicon carbide powder obtained in the step three and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 3-5 hours for reaction at the temperature of 45-58 ℃ and the rotation speed of 500 plus materials per minute;|and step five, respectively dispersing and slurrying the silicon carbide powder obtained by the surface treatment reaction in the step four, physically dispersing, precipitating, separating and drying to obtain the silicon carbide micro powder after surface treatment.|2. The silicon carbide surface treatment method according to claim 1, wherein in the third step, the acid washing process comprises:|the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 50-60 ℃, the pickling time is 2-3 hours, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1;|and ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning times are 4-5 times, and the cleaning time is 1-5 min each time.|3. The silicon carbide surface treatment method according to claim 1, wherein in the third step, the alkali washing process comprises:|the alkaline washing medium is sodium hydroxide with the concentration of 1-10 mol/L, the alkaline washing temperature is 60-70 ℃, and the alkaline washing time is 2-3 h;|and (3) ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4-5 times, and the cleaning time is 1-5 min each time.|4. The silicon carbide surface treatment method as claimed in claim 1, wherein in the fourth step, the organosilicon is silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|5. The silicon carbide surface treatment method according to claim 1, wherein in the fifth step, the silicon carbide powder obtained in the fourth step is mixed with deionized water at room temperature, and the weight ratio of the silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry;|wherein the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1.|6. the silicon carbide surface treatment method as claimed in claim 1, wherein the calcination temperature in the second step is 720 ℃.|7. The silicon carbide surface treatment method according to claim 1, wherein in the third step, the acid washing and the alkali washing are both stirred. (CN110451510)|[0001] Technical Field|[0002] The invention relates to the technical field of silicon carbide micro powder, in particular to a silicon carbide surface treatment method.|[0003] Background|[0004] The silicon carbide fine ceramic has the characteristics of high hardness, high strength, high wear resistance, corrosion resistance, high temperature resistance and the like, and is gradually applied to a plurality of technical fields of aerospace, machinery, metallurgy, energy, environmental protection, chemical engineering, medicine, electronics, military industry and the like. The performance of the silicon carbide fine ceramic is closely related to the quality of silicon carbide raw material micro powder, and the micro powder is generally required to have high purity, uniform particle size distribution, nearly spherical particle shape, difficult agglomeration, good fluidity and good sintering performance.|[0005] The existing industrial production process of the silicon carbide micro powder mainly comprises a series of processes such as smelting, crushing, purification, precision classification and the like, and a shaping procedure is required to be added for the raw material micro powder for the silicon carbide fine ceramics. In the above process, although the separation of silicon carbide micro powder with different particle sizes can be theoretically realized, in practice, complete separation of some particles with very different particle sizes is difficult to realize, for example, a large amount of nano silicon carbide particles (the main component is SiO) are adhered to the surface of micron silicon carbide micro powder particles2And low-purity silicon carbide), while the presence of the nano-scale silicon carbide particles can reduce the purity of the silicon carbide micro powder, affect the fluidity, the dispersibility and the bulk density of the micro powder, and preferentially react with a sintering aid, so that the forming performance and the sintering performance of the silicon carbide micro powder are poor, and the performance of a final silicon carbide fine ceramic product is reduced.|[0006] Disclosure of Invention|[0007] An object of the present invention is to solve at least the above problems and to provide at least the advantages described later.|[0008] The invention also aims to provide a silicon carbide surface treatment method which can specifically remove impurities on the silicon carbide surface, improve the dispersibility of the silicon carbide micro powder and has low cost and low energy consumption.|[0009] In order to achieve the aim, the invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0010] step one, crushing silicon carbide particles and screening silicon carbide powder with the particle size of 5-10 microns;|[0011] placing the silicon carbide powder in a muffle furnace at the temperature of 700-800 ℃ for calcining to remove free carbon on the surface of the silicon carbide powder;|[0012] step three, carrying out acid washing and alkali washing on the silicon carbide powder subjected to carbon removal so as to purify the silicon carbide powder subjected to carbon removal;|[0013] step four, using organic silicon and organic fluorine as surfactants, using ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, then adding the silicon carbide powder obtained in the step three and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 3-5 hours for reaction at the temperature of 45-58 ℃ and the rotation speed of 500 plus materials per minute;|[0014] and step five, respectively dispersing and slurrying the silicon carbide powder obtained by the surface treatment reaction in the step four, physically dispersing, precipitating, separating and drying to obtain the silicon carbide micro powder after surface treatment.|[0015] Preferably, in the third step of the silicon carbide surface treatment method of the present invention, the acid washing process is:|[0016] the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 50-60 ℃, the pickling time is 2-3 hours, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1;|[0017] and ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning times are 4-5 times, and the cleaning time is 1-5 min each time.|[0018] Preferably, in the third step, the alkali washing process is as follows:|[0019] the alkaline washing medium is sodium hydroxide with the concentration of 1-10 mol/L, the alkaline washing temperature is 60-70 ℃, and the alkaline washing time is 2-3 h;|[0020] and (3) ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4-5 times, and the cleaning time is 1-5 min each time.|[0021] Preferably, in the fourth step, the organosilicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0022] Preferably, in the fifth step, the silicon carbide powder obtained in the fourth step is mixed with deionized water at room temperature, and the weight ratio of the silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry;|[0023] wherein the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1.|[0024] preferably, in the silicon carbide surface treatment method according to the present invention, in the second step, the calcination temperature is 720 ℃.|[0025] Preferably, in the third step of the silicon carbide surface treatment method, the acid washing process and the alkali washing process are both stirred.|[0026] The invention at least comprises the following beneficial effects:|[0027] 1. the silicon carbide surface treatment method provided by the invention can effectively remove free carbon, silicon oxide, metal and metal oxide on the surface of the silicon carbide micro powder, thereby specifically removing impurities on the surface of the silicon carbide micro powder.|[0028] 2. The silicon carbide surface treatment method provided by the invention has the advantages of simple process, low cost and low energy consumption, and improves the dispersibility of the silicon carbide micro powder.|[0029] Additional advantages, objects, and features of the invention will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the invention.|[0030] Detailed Description|[0031] The present invention is further described in detail below with reference to examples so that those skilled in the art can practice the invention with reference to the description.|[0032] It will be understood that terms such as "having," "including," and "comprising," as used herein, do not preclude the presence or addition of one or more other elements or groups thereof.|[0033] Example 1|[0034] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0035] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 8 mu m;|[0036] carbon removal: placing the silicon carbide powder in a muffle furnace at the temperature of 700 ℃ for calcining for 4 hours to remove free carbon on the surface of the silicon carbide powder;|[0037] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 50 ℃, the pickling time is 3 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 5min each time;|[0038] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 10mol/L, the alkali washing temperature is 60 ℃, the alkali washing time is 3h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 5min each time;|[0039] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 58 ℃ and the rotating speed of 800r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0040] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry;|[0041] wherein the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1.|[0042] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0043] Example 2|[0044] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0045] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 5 mu m;|[0046] carbon removal: placing the silicon carbide powder in a muffle furnace at the temperature of 720 ℃ for calcining for 3 hours to remove free carbon on the surface of the silicon carbide powder;|[0047] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 60 ℃, the pickling time is 2 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 5 times, and the cleaning time is 1min each time;|[0048] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 5mol/L, the alkali washing temperature is 70 ℃, the alkali washing time is 2h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 5min each time;|[0049] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 50 ℃ and the rotating speed of 700r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0050] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the purified silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry; the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1;|[0051] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0052] Example 3|[0053] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0054] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 10 mu m;|[0055] carbon removal: placing the silicon carbide powder in a muffle furnace at the temperature of 800 ℃ for calcining for 3 hours to remove free carbon on the surface of the silicon carbide powder;|[0056] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 55 ℃, the pickling time is 2.5 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 3min each time;|[0057] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 1mol/L, the alkali washing temperature is 60 ℃, the alkali washing time is 2h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 3min each time;|[0058] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 58 ℃ and the rotating speed of 800r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0059] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the purified silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry; the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1;|[0060] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0061] Example 4|[0062] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0063] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 6 mu m;|[0064] carbon removal: calcining the silicon carbide powder in a muffle furnace at the temperature of 750 ℃ for 3 hours to remove free carbon on the surface of the silicon carbide powder;|[0065] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 60 ℃, the pickling time is 3 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 5 times, and the cleaning time is 5min each time;|[0066] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 10mol/L, the alkali washing temperature is 70 ℃, the alkali washing time is 2h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 5 times, and the cleaning time is 5min each time;|[0067] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 58 ℃ and the rotating speed of 800r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0068] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the purified silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry; the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1;|[0069] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0070] Example 5|[0071] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0072] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 8 mu m;|[0073] carbon removal: placing the silicon carbide powder in a muffle furnace at 780 ℃ for calcination for 4 hours to remove free carbon on the surface of the silicon carbide powder;|[0074] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 60 ℃, the pickling time is 3 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 5min each time;|[0075] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 10mol/L, the alkali washing temperature is 70 ℃, the alkali washing time is 2h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 5 times, and the cleaning time is 1min each time;|[0076] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 58 ℃ and the rotating speed of 800r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0077] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the purified silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry; the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1;|[0078] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0079] The purity of the silicon carbide prepared by the silicon carbide surface treatment methods provided in examples 1 to 5 is greater than 99.52%, the free carbon is less than 0.05%, and the ferric oxide is less than 0.02%.|[0080] While embodiments of the invention have been disclosed above, it is not limited to the applications listed in the description and the embodiments, which are fully applicable in all kinds of fields of application of the invention, and further modifications may readily be effected by those skilled in the art, so that the invention is not limited to the specific details without departing from the general concept defined by the claims and the scope of equivalents. (CN110451510)|[0001] Technical Field|[0002] The invention relates to the technical field of silicon carbide micro powder, in particular to a silicon carbide surface treatment method.|[0003] Background|[0004] The silicon carbide fine ceramic has the characteristics of high hardness, high strength, high wear resistance, corrosion resistance, high temperature resistance and the like, and is gradually applied to a plurality of technical fields of aerospace, machinery, metallurgy, energy, environmental protection, chemical engineering, medicine, electronics, military industry and the like. The performance of the silicon carbide fine ceramic is closely related to the quality of silicon carbide raw material micro powder, and the micro powder is generally required to have high purity, uniform particle size distribution, nearly spherical particle shape, difficult agglomeration, good fluidity and good sintering performance.|[0005] The existing industrial production process of the silicon carbide micro powder mainly comprises a series of processes such as smelting, crushing, purification, precision classification and the like, and a shaping procedure is required to be added for the raw material micro powder for the silicon carbide fine ceramics. In the above process, although the separation of silicon carbide micro powder with different particle sizes can be theoretically realized, in practice, complete separation of some particles with very different particle sizes is difficult to realize, for example, a large amount of nano silicon carbide particles (the main component is SiO) are adhered to the surface of micron silicon carbide micro powder particles2And low-purity silicon carbide), while the presence of the nano-scale silicon carbide particles can reduce the purity of the silicon carbide micro powder, affect the fluidity, the dispersibility and the bulk density of the micro powder, and preferentially react with a sintering aid, so that the forming performance and the sintering performance of the silicon carbide micro powder are poor, and the performance of a final silicon carbide fine ceramic product is reduced.|[0006] Disclosure of Invention|[0007] An object of the present invention is to solve at least the above problems and to provide at least the advantages described later.|[0008] The invention also aims to provide a silicon carbide surface treatment method which can specifically remove impurities on the silicon carbide surface, improve the dispersibility of the silicon carbide micro powder and has low cost and low energy consumption.|[0009] In order to achieve the aim, the invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0010] step one, crushing silicon carbide particles and screening silicon carbide powder with the particle size of 5-10 microns;|[0011] placing the silicon carbide powder in a muffle furnace at the temperature of 700-800 ℃ for calcining to remove free carbon on the surface of the silicon carbide powder;|[0012] step three, carrying out acid washing and alkali washing on the silicon carbide powder subjected to carbon removal so as to purify the silicon carbide powder subjected to carbon removal;|[0013] step four, using organic silicon and organic fluorine as surfactants, using ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, then adding the silicon carbide powder obtained in the step three and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 3-5 hours for reaction at the temperature of 45-58 ℃ and the rotation speed of 500 plus materials per minute;|[0014] and step five, respectively dispersing and slurrying the silicon carbide powder obtained by the surface treatment reaction in the step four, physically dispersing, precipitating, separating and drying to obtain the silicon carbide micro powder after surface treatment.|[0015] Preferably, in the third step of the silicon carbide surface treatment method of the present invention, the acid washing process is:|[0016] the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 50-60 ℃, the pickling time is 2-3 hours, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1;|[0017] and ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning times are 4-5 times, and the cleaning time is 1-5 min each time.|[0018] Preferably, in the third step, the alkali washing process is as follows:|[0019] the alkaline washing medium is sodium hydroxide with the concentration of 1-10 mol/L, the alkaline washing temperature is 60-70 ℃, and the alkaline washing time is 2-3 h;|[0020] and (3) ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4-5 times, and the cleaning time is 1-5 min each time.|[0021] Preferably, in the fourth step, the organosilicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0022] Preferably, in the fifth step, the silicon carbide powder obtained in the fourth step is mixed with deionized water at room temperature, and the weight ratio of the silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry;|[0023] wherein the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1.|[0024] preferably, in the silicon carbide surface treatment method according to the present invention, in the second step, the calcination temperature is 720 ℃.|[0025] Preferably, in the third step of the silicon carbide surface treatment method, the acid washing process and the alkali washing process are both stirred.|[0026] The invention at least comprises the following beneficial effects:|[0027] 1. the silicon carbide surface treatment method provided by the invention can effectively remove free carbon, silicon oxide, metal and metal oxide on the surface of the silicon carbide micro powder, thereby specifically removing impurities on the surface of the silicon carbide micro powder.|[0028] 2. The silicon carbide surface treatment method provided by the invention has the advantages of simple process, low cost and low energy consumption, and improves the dispersibility of the silicon carbide micro powder.|[0029] Additional advantages, objects, and features of the invention will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the invention.|[0030] Detailed Description|[0031] The present invention is further described in detail below with reference to examples so that those skilled in the art can practice the invention with reference to the description.|[0032] It will be understood that terms such as "having," "including," and "comprising," as used herein, do not preclude the presence or addition of one or more other elements or groups thereof.|[0033] Example 1|[0034] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0035] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 8 mu m;|[0036] carbon removal: placing the silicon carbide powder in a muffle furnace at the temperature of 700 ℃ for calcining for 4 hours to remove free carbon on the surface of the silicon carbide powder;|[0037] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 50 ℃, the pickling time is 3 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 5min each time;|[0038] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 10mol/L, the alkali washing temperature is 60 ℃, the alkali washing time is 3h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 5min each time;|[0039] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 58 ℃ and the rotating speed of 800r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0040] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry;|[0041] wherein the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1.|[0042] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0043] Example 2|[0044] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0045] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 5 mu m;|[0046] carbon removal: placing the silicon carbide powder in a muffle furnace at the temperature of 720 ℃ for calcining for 3 hours to remove free carbon on the surface of the silicon carbide powder;|[0047] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 60 ℃, the pickling time is 2 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 5 times, and the cleaning time is 1min each time;|[0048] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 5mol/L, the alkali washing temperature is 70 ℃, the alkali washing time is 2h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 5min each time;|[0049] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 50 ℃ and the rotating speed of 700r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0050] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the purified silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry; the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1;|[0051] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0052] Example 3|[0053] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0054] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 10 mu m;|[0055] carbon removal: placing the silicon carbide powder in a muffle furnace at the temperature of 800 ℃ for calcining for 3 hours to remove free carbon on the surface of the silicon carbide powder;|[0056] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 55 ℃, the pickling time is 2.5 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 3min each time;|[0057] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 1mol/L, the alkali washing temperature is 60 ℃, the alkali washing time is 2h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 3min each time;|[0058] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 58 ℃ and the rotating speed of 800r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0059] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the purified silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry; the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1;|[0060] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0061] Example 4|[0062] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0063] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 6 mu m;|[0064] carbon removal: calcining the silicon carbide powder in a muffle furnace at the temperature of 750 ℃ for 3 hours to remove free carbon on the surface of the silicon carbide powder;|[0065] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 60 ℃, the pickling time is 3 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 5 times, and the cleaning time is 5min each time;|[0066] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 10mol/L, the alkali washing temperature is 70 ℃, the alkali washing time is 2h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 5 times, and the cleaning time is 5min each time;|[0067] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 58 ℃ and the rotating speed of 800r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0068] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the purified silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry; the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1;|[0069] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0070] Example 5|[0071] The invention discloses a silicon carbide surface treatment method, which comprises the following steps:|[0072] crushing: crushing silicon carbide particles and screening silicon carbide powder with the particle size of 8 mu m;|[0073] carbon removal: placing the silicon carbide powder in a muffle furnace at 780 ℃ for calcination for 4 hours to remove free carbon on the surface of the silicon carbide powder;|[0074] acid washing: pickling the silicon carbide powder after carbon removal, wherein the pickling medium is mixed acid of concentrated sulfuric acid and hydrofluoric acid, the pickling temperature is 60 ℃, the pickling time is 3 hours, mechanical stirring is carried out in the pickling process, and the volume ratio of the concentrated sulfuric acid to the hydrofluoric acid is 2: 1; ultrasonically cleaning the silicon carbide powder subjected to acid cleaning by using deionized water, wherein the cleaning frequency is 4 times, and the cleaning time is 5min each time;|[0075] alkali washing: carrying out alkali washing on the silicon carbide powder after acid washing, wherein the alkali washing medium is sodium hydroxide with the concentration of 10mol/L, the alkali washing temperature is 70 ℃, the alkali washing time is 2h, and mechanical stirring is carried out in the alkali washing process; ultrasonically cleaning the silicon carbide powder subjected to alkali cleaning by using deionized water, wherein the cleaning frequency is 5 times, and the cleaning time is 1min each time;|[0076] surface treatment: the method comprises the steps of taking organic silicon and organic fluorine as surfactants, taking ethanol and water as solvents, adding the organic silicon, the organic fluorine, the ethanol and the water into a surface treatment reaction kettle according to the volume ratio of 3:1:4:1, adding silicon carbide powder obtained by decarbonization and purification and the solvents into the surface treatment reaction kettle according to the volume ratio of 1:2, and fully stirring for 5 hours at the temperature of 58 ℃ and the rotating speed of 800r/min for reaction, wherein the organic silicon is a silane coupling agent Z-6040, and the organic fluorine is fluorocarboxylic acid BYK-P104S.|[0077] Dispersing and slurrying: mixing the silicon carbide powder obtained after surface treatment with deionized water at room temperature, wherein the weight ratio of the purified silicon carbide powder to the deionized water is 1: 1.5, adding a chemical dispersant, fully stirring to fully disperse and slurry the silicon carbide powder in deionized water to obtain silicon carbide slurry, and then physically dispersing the silicon carbide slurry; the weight ratio of the chemical dispersant to the purified silicon carbide powder is 1: 10, the chemical dispersant is a mixture of a polycarboxylic acid type surfactant and a beta-sodium sulfonate formaldehyde condensate, and the weight ratio of the polycarboxylic acid type surfactant to the beta-sodium sulfonate formaldehyde condensate is 1: 1;|[0078] and (3) finished product: and (3) sequentially carrying out physical dispersion, precipitation separation and drying on the silicon carbide powder subjected to dispersion and slurrying to obtain the silicon carbide micro powder subjected to surface treatment.|[0079] The purity of the silicon carbide prepared by the silicon carbide surface treatment methods provided in examples 1 to 5 is greater than 99.52%, the free carbon is less than 0.05%, and the ferric oxide is less than 0.02%.|[0080] While embodiments of the invention have been disclosed above, it is not limited to the applications listed in the description and the embodiments, which are fully applicable in all kinds of fields of application of the invention, and further modifications may readily be effected by those skilled in the art, so that the invention is not limited to the specific details without departing from the general concept defined by the claims and the scope of equivalents. Family Number|(86637865)|86637865|Abstract|(CN110451510 A)|The invention discloses a silicon carbide surface treatment method which comprises the following steps : I , crushing silicon carbide granules , and screening silicon carbide powder of which the particlesize is 5-10 [ mu ] m ; II , calcining the silicon carbide powder in a muffle furnace of 700-800 DEG C so as to remove free carbon on the surface of the silicon carbide powder ; III , performing acid pickling and alkali wash on the silicon carbide powder after carbon removal so as to purify the silicon carbide powder after carbon removal ; and IV , respectively performing dispersion pulping , physical dispersion , precipitate separation and drying on the silicon carbide powder after purification , so as to obtain silicon carbide micro powder after surface treatment . By adopting the silicon carbide surface treatment method disclosed by the invention , impurities on the surface of silicon carbide can be specifically removed , the dispersibility of the silicon carbide micro powder can be improved , in addition , the cost is low , and the energy consumption is low . |CPC codes|(CN110451510 A)|C01B - 032/956 |IPC codes|(CN110451510 A)|C01B - 032/956 | Materials, metallurgy C01B-032/956|C04B-035/565|C04B-035/626/05 C01B-032/956|C04B-035/565|C04B-035/626/05 C01B-032/956|C04B-035/565|C04B-035/626 C01B-032/956|C04B-035/565|C04B-035/626 CN110983446|CN118083982|CN113956048|CN111606720|CN111196724|CN114956087B|CN113502407B CN110983446 88201860 WHO=Examiner SELF=N CAT=X|CN118083982 109951726 WHO=Examiner SELF=N CAT=A|CN113956048 98357508 WHO=Examiner SELF=N CAT=A|CN111606720 90455684 WHO=Examiner SELF=Y CAT=A|CN111196724 88933788 WHO=Examiner SELF=Y CAT=A|CN114956087B 101562019 WHO=Examiner SELF=N|CN113502407B 96508276 WHO=Examiner SELF=N LAPSED (CN110451510)|LAPSED DEAD (CN110451510)|DEAD (CN110451510)|LEGAL DETAILS FOR CN110451510|Actual or expected expiration date=2021-08-17|Legal state=DEAD|Status=LAPSED|Event publication date=2019-05-21|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201910425889|Application date=2019-05-21|Standardized application number=2019CN-0425889|Event publication date=2019-11-15|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN110451510|Publication stage code=A|Publication date=2019-11-15|Standardized publication number=CN110451510|Event publication date=2019-11-15|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2020-02-14|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2021-08-17|Event code=CN/WW01|Event indicator=Neg|Event group=Event indicating Not In Force|Withdrawal of patent application after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRdg17h1Q3d+Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=Bsvld9ty6Dadu1u%252Fd8QdWpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN110451510)|CN (CN110451510)|NAME=HUNAN TAIZI NEW MATERIAL TECHNOLOGY CO., LTD. , COUNTRY=CN (CN110451510)|NAME=WANG XINAI;BEIJING SKYINTEL PATENT AGENCY , REG=11638 (CN110451510)|NAME=LIU JUN|NAME=LIU ZHENHUA|NAME=ZHANG HAI 0 1 Titre: (CN110451510)|Silicon carbide surface treatment method Résumé: (CN110451510)|The invention discloses a silicon carbide surface treatment method which comprises the following steps: I, crushing silicon carbide granules, and screening silicon carbide powder of which the particlesize is 5-10[mu] m; II, calcining the silicon carbide powder in a muffle furnace of 700-800 DEG C so as to remove free carbon on the surface of the silicon carbide powder; III, performing acid pickling and alkali wash on the silicon carbide powder after carbon removal so as to purify the silicon carbide powder after carbon removal; and IV, respectively performing dispersion pulping, physical dispersion, precipitate separation and drying on the silicon carbide powder after purification, so as to obtain silicon carbide micro powder after surface treatment. By adopting the silicon carbide surface treatment method disclosed by the invention, impurities on the surface of silicon carbide can be specifically removed, the dispersibility of the silicon carbide micro powder can be improved, in addition, the cost is low, and the energy consumption is low. 63 Abstract gpt-4o-mini no The article focuses on a surface treatment method for silicon carbide, which does not relate to accelerated weathering or CO₂ capture.
69 CN202510936450 CN202510936450 CN120551173 115814465 CN120551173 A 2025-08-29 [CN120551173] 2025-07-08 2025-07-08 2025-08-29 (CN120551173)|2045-07-08 (CN120551173)|Garden waste carbon sink storage method for improving planting soil (CN120551173)|The invention discloses a garden waste carbon sequestration and storage method for improving planting soil, which comprises the following steps: collecting, classifying and crushing garden wastes, classifying different collected objects, carrying out incomplete carbonization treatment, merging roots, stems and leaves of herbaceous plants and leaves of woody plants into a first type of garden wastes, and ensuring that the carbonization rate is 75-83%; roots, branches and stems of woody plants are combined into second-class garden waste, and the carbonization rate is 55-65%; and mixing carbonized products according to a weight ratio of 1: (2-3) to obtain the carbon sequestration plant material for improving the planting soil. The carbon sequestration planting material has a good carbon sequestration effect, so that the carbon sequestration planting material is not easily and completely degraded in nature, meanwhile, due to the fact that the carbon sequestration planting material is not completely carbonized, part of lignin can be retained and can be slowly decomposed, the self structure is not easily collapsed, high porosity is maintained, long-acting water retention and fertilizer retention can be achieved, meanwhile, attachment growth of microorganisms can be facilitated, and the vitality of planting soil is kept. YANGZHOU POLYTECHNIC INSTITUTE (CN120551173)|YANGZHOU POLYTECHNIC INSTITUTE ([CN]) YU JINGJING (CN120551173)|YU JINGJING (CN120551173)|DONG XUDONG;NANJING SUKE INTELLECTUAL PROPERTY AGENT. LTD.|Reg. Nb: 32102 (CN120551173)|The invention aims to provide a garden waste carbon sink sealing method for planting soil improvement, which can realize long-term carbon fixation, improve soil, enable planting soil to be breathable, retain water and fertilizer, and provide a good living environment for plant and soil microorganism growth.|The simple tree leaves are carbonized, the porosity is higher, but the strength of the carbon skeleton is poor, and after the simple tree leaves are mixed with soil for improvement, the simple tree leaves are easy to generate structural damage and collapse of pores under the action of water, oxygen and microorganisms, so that the improved soil is disabled.How to effectively fix carbon in garden waste and apply the carbon to soil improvement so that the soil can keep suitable plant and bacteria growth for a long time is a technical problem to be solved at present.| (CN120551173)|1. The garden waste carbon sink sealing method for planting soil improvement is characterized by comprising the following steps of: S1, collecting garden waste, carrying out rough separation and drying, combining roots, stems and leaves of herbaceous plants and leaves of woody plants into a first class, and combining the roots, branches and stems of the woody plants into a second class during rough separation, wherein the moisture content in the materials is lower than 15 percent; S2, shredding the first type of garden waste treated in the step S1 to ensure that the average plane size is 6-10mm, stirring uniformly, sampling, weighing and pyrolyzing in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to ensure that the first type of garden waste is dehydrated, the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, the pyrolysis device is kept warm, meanwhile, the gas generated by pyrolysis is released, the liquid oil in the effluent product is led out, the rest solid matters are continuously weighed, when the constant weight of the pyrolyzed solid product lasts for 30min, stopping pyrolysis, recording the heat preservation time corresponding to the weight loss of the solid product, comparing the weight loss before and after carbonization of the material, equally dividing the weight loss into 100 parts, and regarding that the carbonization rate is increased by 1% for 1 part reduction, and determining the carbonization rate as a first target time; S3, pyrolyzing the first type of garden waste remained in the step S2 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, then the pyrolysis device is kept at the temperature, and after the first target time, the carbonization rate of the remained solid matters is 75-83%; S4, crushing the second type of garden waste after the step S1 into blocks with the maximum three-dimensional size of less than 3cm, sampling, weighing and pyrolyzing in an anaerobic environment, rapidly heating to 200 ℃ during pyrolysis, preserving heat for 15-20min to enable the blocks to lose water, slowly heating to 450-480 ℃ at the heating rate of 10-15 ℃ per min, preserving heat of a pyrolysis device, simultaneously releasing gas generated by pyrolysis of the blocks, introducing liquid oil in a product, continuously weighing the rest solid matters, stopping pyrolysis when the constant weight of the solid product after pyrolysis lasts for 30min, comparing the weights before and after carbonization of the material, equally dividing the weight loss part into 100 equal parts, and determining the carbonization rate as 1% for each 1% reduction and the carbonization rate as a second target time; S5, pyrolyzing the second type of garden waste remained in the step S4 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 450-480 ℃ at the temperature rise rate of 10-15 ℃ per min, and the pyrolysis device is kept for a second target time, so that the carbonization rate of the remained solid matters is 55-65%; s6, mixing the solid matters obtained in the steps S3 and S5 according to the weight ratio of 1 (2-3) to obtain the carbon sink plant material for improving the planting soil. | (CN120551173)|The invention discloses a garden waste carbon sequestration method for planting soil improvement, which comprises the steps of collecting and classifying garden waste, crushing the garden waste, carrying out incomplete carbonization treatment on different collected matters, combining roots, stems and leaves of herbaceous plants and leaves of woody plants into first-class garden waste with carbonization rate of 75-83%, combining roots, branches and stems of woody plants into second-class garden waste with carbonization rate of 55-65%, and mixing carbonized products according to weight ratio of 1 (2-3) to obtain the carbon sequestration plant material for planting soil improvement.|The invention relates to a method for treating garden waste, in particular to a carbon sequestration method for garden waste and application of the method in soil improvement.| (CN120551173)|GARDEN WASTE(100,69)|CARBON SINK(100,21)|PLANTING SOIL(100,17)|GARDEN WASTE CARBON SINK(100,5)|WOODY PLANT(83,10)|INCOMPLETE CARBONIZATION TREATMENT(75,1)|TREE LEAF(74,5)|ANAEROBIC ENVIRONMENT(72,12)|PLANTED SOIL IMPROVEMENT(72,6)|PYROLYSIS(70,26)|CARBONIZATION(64,32)|STOPPING PYROLYSIS(63,5)|GARDEN WASTE CLASSIFICATION(62,1)|SOIL MICROORGANISM GROWTH(62,1)|CARBON SEQUESTRATION(45,5)|CLASS GARDEN WASTE(42,8)|BACTERIA GROWTH(42,1)|ROUGH SEPARATION(41,6)|MATTER COLLECTION(41,1)|GROUND(37,9)|GARDEN WASTE COLLECTION(35,3)|GARDEN WASTE TREATMENT(35,1)|REMAINED SOLID MATTER(34,6)|CARBONIZED PRODUCT(32,2)|HEAT PRESERVATION(31,8)|HERBACEOUS PLANT(31,6)|MICROORGANISM ADHESION(31,3)|PYROLYSIS LAST(31,3)|LIVING ENVIRONMENT(31,2)|MOISTURE CONTENT(30,2)|BLOCK PYROLYSIS(28,2)|EFFLUENT PRODUCT(28,2)|REST SOLID MATTER(26,6)|FERTILIZER(26,1)|STRUCTURAL DAMAGE(26,1)|MATERIAL CARBONIZATION(25,5)|GARDEN WASTE CARBON SEQUESTRATION(25,3)|CARBONIZATION RATE(23,20)|POROSITY(23,17)|SAMPLING(23,6)|STEM(23,5)|SEALING CARBON SINK(23,2)|LIQUID OIL(22,6)|SOIL IMPROVEMENT(21,6)|PYROLYZED SOLID PRODUCT LAST(21,2)|SOLID PRODUCT(20,6)|INCOMPLETELY CARBONIZED GARDEN WASTE(19,3)|MICROORGANISM(18,5)|SOLID MATTER(17,3)|PRODUCT LAST(17,2)|CARBON SKELETON(17,1)|TARGET TIME(15,12)|WEIGHT LOSS(14,17)|INCOMPLETE CARBONIZATION GARDEN WASTE(14,2)|TEMPERATURE RISE(13,8)|LEAVE CARBONIZATION(13,4)|PORE(13,3)|SAMPLE WEIGHT(13,3)|PLANTING SOIL FERTILIZER RETENTION(13,1)|CARBON SEQUESTRATION PLANT MATERIAL(12,1)|CARBON SINK PLANT MATERIAL(11,13)|CARBON FIXATION(11,4)|GARDEN WASTE CLASS(11,4)|FLUIDIZED BED(11,3)|REACTOR(11,3)|TYPE GARDEN WASTE(11,2)|FIXED BED(10,3)|MEDIAN PLANE SIZE(10,3)|CAMPUS FALLEN LEAVE(10,1)|CARBONIZED LEAVE POROSITY(10,1)|FRENCH PHENIX TREE(10,1)|TUBE FURNACE(10,1)|CARBON FIXING(9,3)|PLANT MATERIAL(8,15)|WEIGHT RATIO(8,10)|HEAT PRESERVATION TIME(8,3)|SELF STRUCTURE(8,2)|LONG TERM CARBON FIXATION(8,1)|WOODY PLANT LEAVE(8,1)|CONSTANT WEIGHT(7,3)|PART REDUCTION(7,2)|VOLUME MIXING RATIO(7,2)|CARBONIZATION INDEX(7,1)|PYROLYZING PRESERVING HEAT(7,1)|VEGETATION RESTORATION(7,1)|PYROLYSIS TEMPERATURE(6,4)|TUBULAR FURNACE(6,2)|CAMPUS TREE SPECIES(6,1)|DOMINANT PORE(6,1)|PORE CANAL(6,1)|SOIL MICROORGANISM(6,1)|TREE TRUNK INDEX(6,1)|TRUNK PYROLYSIS DATA(6,1)|LONG ACTING WATER(5,3)|MACROPORE(5,2)|BIOFILM ATTACHMENT(5,1)|FALLEN LEAVE RATIO(5,1)|GARDEN SOIL(5,1)|GRAPHITIZED CARBON(5,1)|PLANT BIOMASS(5,1)|PLANT ROOTING(5,1)|PORE CONTRAST INDEX(5,1)|RESIDUAL LIGNIN(5,1)|TREE PYROLYSIS DATA(5,1)|HEMICELLULOSE(4,2)|THREE DIMENSIONAL SIZE(4,2)|ACCURATE MEASUREMENT(4,1)|ADSORPTION CAPACITY(4,1)|CARBON DEPOSIT CARRIER(4,1)|CARBONIZATION SPEED(4,1)|DENSE WOOD(4,1)|GENERATED MICROPORE(4,1)|METAPHASE(4,1)|MIXED LEAF(4,1)|MIXED TRUNK(4,1)|NATURAL GROWTH(4,1)|NATURAL SUBSTANCE(4,1)|ONLY TRUNK(4,1)|PORE DISTRIBUTION(4,1)|SLOW DECOMPOSITION(4,1)|CHARCOAL(3,2)|MAXIMUM THREE DIMENSIONAL SIZE(3,2)|POROSITY MEASUREMENT(3,2)| (CN120551173)|1. The garden waste carbon sink sealing method for planting soil improvement is characterized by comprising the following steps of:| S1, collecting garden waste, carrying out rough separation and drying, combining roots, stems and leaves of herbaceous plants and leaves of woody plants into a first class, and combining the roots, branches and stems of the woody plants into a second class during rough separation, wherein the moisture content in the materials is lower than 15 percent; | S2, shredding the first type of garden waste treated in the step S1 to ensure that the average plane size is 6-10mm, stirring uniformly, sampling, weighing and pyrolyzing in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to ensure that the first type of garden waste is dehydrated, the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, the pyrolysis device is kept warm, meanwhile, the gas generated by pyrolysis is released, the liquid oil in the effluent product is led out, the rest solid matters are continuously weighed, when the constant weight of the pyrolyzed solid product lasts for 30min, stopping pyrolysis, recording the heat preservation time corresponding to the weight loss of the solid product, comparing the weight loss before and after carbonization of the material, equally dividing the weight loss into 100 parts, and regarding that the carbonization rate is increased by 1% for 1 part reduction, and determining the carbonization rate as a first target time; | S3, pyrolyzing the first type of garden waste remained in the step S2 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, then the pyrolysis device is kept at the temperature, and after the first target time, the carbonization rate of the remained solid matters is 75-83%; | S4, crushing the second type of garden waste after the step S1 into blocks with the maximum three-dimensional size of less than 3cm, sampling, weighing and pyrolyzing in an anaerobic environment, rapidly heating to 200 ℃ during pyrolysis, preserving heat for 15-20min to enable the blocks to lose water, slowly heating to 450-480 ℃ at the heating rate of 10-15 ℃ per min, preserving heat of a pyrolysis device, simultaneously releasing gas generated by pyrolysis of the blocks, introducing liquid oil in a product, continuously weighing the rest solid matters, stopping pyrolysis when the constant weight of the solid product after pyrolysis lasts for 30min, comparing the weights before and after carbonization of the material, equally dividing the weight loss part into 100 equal parts, and determining the carbonization rate as 1% for each 1% reduction and the carbonization rate as a second target time; | S5, pyrolyzing the second type of garden waste remained in the step S4 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 450-480 ℃ at the temperature rise rate of 10-15 ℃ per min, and the pyrolysis device is kept for a second target time, so that the carbonization rate of the remained solid matters is 55-65%; | s6, mixing the solid matters obtained in the steps S3 and S5 according to the weight ratio of 1 (2-3) to obtain the carbon sink plant material for improving the planting soil. |2. The method for sealing carbon sink of garden waste for improving planting soil according to claim 1, wherein in the steps S2 and S4, the constant weight is determined that the weight loss is lower than 5% of the sampling weight within 30 min.|3. The method for carbon sequestration of garden waste for soil improvement according to claim 1, wherein the reactor used for pyrolysis is a fluidized bed, a fixed bed or a tube furnace.|4. The method for sealing carbon sink of garden waste for improving planting soil according to claim 1, wherein the volume mixing ratio of carbon sink plant material to planting soil is (3-8): 1.|5. The method for carbon sequestration of garden waste for improving planting soil according to claim 1, wherein in step S1, only leaves are collected as first type garden waste, and only trunks are collected as first type garden waste. (CN120551173)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to a method for treating garden waste, in particular to a carbon sequestration method for garden waste and application of the method in soil improvement.|BACKGROUND ART|[0002] Since the content of CO 2 gas in nature is gradually increased due to the large-scale utilization of petroleum and coal, CO 2 is a greenhouse gas, and the content change in the atmosphere may have an adverse effect on the global environment, the concept of carbon sink, which generally refers to the process, activity and mechanism of removing carbon dioxide from the air, has been proposed in recent years. Carbon sink is a carbon deposit carrier in nature, and mainly utilizes photosynthesis of plants to absorb carbon dioxide in the atmosphere and fix the carbon dioxide in vegetation and soil through measures such as afforestation, forest management and vegetation restoration, so that the concentration of greenhouse gases in the atmosphere is reduced.|[0003] The existing garden waste mainly comprises leaves and branches which naturally wither and are manually pruned, and is natural substances, mainly comprises cellulose, lignin and the like, and in the nature, the leaves and branches are naturally decomposed by various bacteria and become CO 2 and H 2 O to enter natural circulation, so that a dynamic balance is formed, how to reduce the time of returning biological carbon fixation to the nature again or delay the time of returning the biological carbon fixation to the nature is reduced, and the concentration of greenhouse gases in the atmosphere can be kept to be relatively low in theory. Plants are carbonized, and can be kept for decades to thousands of years in nature, depending on the degree of carbonization.|[0004] The existing soil, especially clay, has low porosity, is easy to harden, is unfavorable for plant rooting and bacterial growth, and needs to be improved.|[0005] In the prior art, a method for improving soil by charcoal is reported, but the charcoal is mainly formed by insufficient combustion of main stems and branches of trees, has larger pores, low porosity compared with carbonized leaves, small total pore volume, smaller end points and fewer surface functional groups, so that the adsorption capacity of materials is weaker, the capacities of water retention, fertilizer retention and oxygen supply microorganisms are weaker, and an optimal soil improvement scheme cannot be provided. The simple tree leaves are carbonized, the porosity is higher, but the strength of the carbon skeleton is poor, and after the simple tree leaves are mixed with soil for improvement, the simple tree leaves are easy to generate structural damage and collapse of pores under the action of water, oxygen and microorganisms, so that the improved soil is disabled.|[0006] How to effectively fix carbon in garden waste and apply the carbon to soil improvement so that the soil can keep suitable plant and bacteria growth for a long time is a technical problem to be solved at present.|DISCLOSURE|Disclosure of Invention|[0007] The invention aims to provide a garden waste carbon sink sealing method for planting soil improvement, which can realize long-term carbon fixation, improve soil, enable planting soil to be breathable, retain water and fertilizer, and provide a good living environment for plant and soil microorganism growth.|[0008] The invention aims to realize the method for sealing and storing carbon sink of garden waste for improving planting soil, which comprises the following steps:|[0009] S1, collecting garden waste, carrying out rough separation and drying, combining roots, stems and leaves of herbaceous plants and leaves of woody plants into a first class, and combining the roots, branches and stems of the woody plants into a second class during rough separation, wherein the moisture content in the materials is lower than 15 percent; |[0010] S2, shredding the first type of garden waste treated in the step S1 to ensure that the average plane size is 6-10mm, stirring uniformly, sampling, weighing and pyrolyzing in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to ensure that the first type of garden waste is dehydrated, the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, the pyrolysis device is kept warm, meanwhile, the gas generated by pyrolysis is released, the liquid oil in the effluent product is led out, the rest solid matters are continuously weighed, when the constant weight of the pyrolyzed solid product lasts for 30min, stopping pyrolysis, recording the heat preservation time corresponding to the weight loss of the solid product, comparing the weight loss before and after carbonization of the material, equally dividing the weight loss into 100 parts, and regarding that the carbonization rate is increased by 1% for 1 part reduction, and determining the carbonization rate as a first target time; |[0011] S3, pyrolyzing the first type of garden waste remained in the step S2 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, then the pyrolysis device is kept at the temperature, and after the first target time, the carbonization rate of the remained solid matters is 75-83%; |[0012] S4, crushing the second type of garden waste after the step S1 into blocks with the maximum three-dimensional size of less than 3cm, sampling, weighing and pyrolyzing in an anaerobic environment, rapidly heating to 200 ℃ during pyrolysis, preserving heat for 15-20min to enable the blocks to lose water, slowly heating to 450-480 ℃ at the heating rate of 10-15 ℃ per min, preserving heat of a pyrolysis device, simultaneously releasing gas generated by pyrolysis of the blocks, introducing liquid oil in a product, continuously weighing the rest solid matters, stopping pyrolysis when the constant weight of the solid product after pyrolysis lasts for 30min, comparing the weights before and after carbonization of the material, equally dividing the weight loss part into 100 equal parts, and determining the carbonization rate as 1% for each 1% reduction and the carbonization rate as a second target time; |[0013] S5, pyrolyzing the second type of garden waste remained in the step S4 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 450-480 ℃ at the temperature rise rate of 10-15 ℃ per min, and the pyrolysis device is kept for a second target time, so that the carbonization rate of the remained solid matters is 55-65%; |[0014] s6, mixing the solid matters obtained in the steps S3 and S5 according to the weight ratio of 1 (2-3) to obtain the carbon sink plant material for improving the planting soil. |[0015] Further, in steps S2 and S4, it is determined that the weight loss of less than 5% of the sampled weight within 30 minutes is constant weight.|[0016] Further, in the case of improving the planting soil, the mixing ratio of the carbon sink plant material to the planting soil by volume is (3-8): 1.|[0017] Pyrolysis of plant biomass is a thermochemical process in which hemicellulose is first decomposed at a lower temperature, cellulose is decomposed in a medium temperature range, and lignin is finally decomposed at a higher temperature. The biological structure, chemical composition and physical characteristics of the tree leaf and the tree trunk are obviously different, the tree leaf is a leaf structure with parenchyma as a main part, and the tree trunk is a compact wood structure with a wood part as a main part, so that the carbonization process, the carbonization speed and the characteristic indexes of the tree trunk are obviously different. The leaves are pyrolyzed at a relatively low temperature, while the trunks are pyrolyzed at a relatively high temperature, so that the aim is to obtain a better carbon fixing effect, the yield of the biochar material is reduced due to the fact that the excessive pyrolysis temperature is increased, but the total structure of the biochar can be increased due to the fact that the pyrolysis temperature is increased, and therefore the specific surface area of the biochar is increased. The lower pyrolysis temperature can lead the biochar to have the characteristic of hydrophilicity. According to the invention, different pyrolysis temperatures are adopted for the first-class garden waste and the second-class garden waste, so that the aim is to ensure high-efficiency carbon fixation and reduce volatilization of oil and gas, and the organic matters are kept with more weight proportion of converted carbon as much as possible under the condition of fixed carbonization rate, thereby ensuring the carbon sink effect. Compared with the prior art, the invention has the beneficial effects that the roots, stems and leaves of herbaceous plants and the leaves of woody plants are combined into first-class garden waste, the carbonization rate is 75-83%, the roots, branches and stems of woody plants are combined into second-class garden waste, the carbonization rate is 55-65%, and carbonized products are mixed according to the weight ratio of 1 (2-3), so as to obtain the carbon sink plant material for planting soil improvement. The carbon sink plant material has good carbon fixing effect, so that the carbon sink plant material is not easy to degrade completely in nature, meanwhile, as the carbon sink plant material is not completely carbonized, part of lignin can be decomposed slowly, the self structure is not easy to collapse, high porosity is maintained, long-acting water and fertilizer retention can be realized, microorganism adhesion and growth can be facilitated, and the activity of planting soil can be maintained.|INVENTION MODE|Detailed Description|[0018] A garden waste carbon sink sealing method for planting soil improvement is carried out according to the following steps:|[0019] S1, collecting garden waste, carrying out rough separation and drying, combining roots, stems and leaves of herbaceous plants and leaves of woody plants into a first class during rough separation, combining the roots, branches and stems of woody plants into a second class, drying to ensure that the water content in the materials is lower than 15%, also discarding the herbaceous plants, only collecting the leaves as the first class of garden waste, taking the trunk as the second class of garden waste, classifying branches with diameters of more than 0.8cm into the second class of garden waste, and classifying branches with diameters of less than 0.8cm into the first class of garden waste. |[0020] S2, cutting the garden waste of the first type treated in the step S1 to ensure that the average plane size is 6-10mm, stirring uniformly, sampling, weighing and pyrolyzing in an anaerobic environment, wherein a reactor used for pyrolyzing is a fluidized bed, a fixed bed or a tubular furnace, heating to 200 ℃ rapidly during pyrolyzing, preserving heat for 15-20min to ensure that the water is lost, heating to 380-400 ℃ slowly at the heating rate of 10-15 ℃ per min, preserving heat of a pyrolyzing device, simultaneously releasing gas generated by pyrolysis, guiding liquid oil in a discharged product, continuously weighing the rest solid matters, stopping pyrolyzing when the constant weight of the pyrolyzed solid product is continuously maintained for 30min, recording the heat preservation time corresponding to the weight loss of the solid product, comparing the weight before and after carbonization of the material, dividing the weight loss into 100 equal parts, and determining that the carbonization rate is increased by 1% every 1% and the carbonization rate is 75-83% as a first target time;|[0021] S3, pyrolyzing the first type of garden waste remained in the step S2 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, then the pyrolysis device is kept at the temperature, and after the first target time, the carbonization rate of the remained solid matters is 75-83%; |[0022] S4, crushing the second type of garden waste after the step S1 into blocks with the largest three-dimensional size of less than 3cm, sampling, weighing and pyrolyzing in an anaerobic environment, wherein a reactor used for pyrolysis is a fluidized bed, a fixed bed or a tubular furnace, quickly heating to 200 ℃ during pyrolysis, preserving heat for 15-20min to enable the water to be lost, slowly heating to 450-480 ℃ at the heating rate of 10-15 ℃ per min, preserving heat of a pyrolysis device, simultaneously releasing gas generated by pyrolysis of the pyrolysis device, introducing liquid oil in a product, continuously weighing the rest solid matters, stopping pyrolysis when the constant weight of the solid product after pyrolysis lasts for 30min, comparing the weight of the material before and after carbonization, equally dividing the weight loss part into 100 equal parts, and determining that the carbonization rate is increased by 1% when the carbonization rate is reduced by 1%, and determining the carbonization rate as a second target time by 55-65%; |[0023] S5, pyrolyzing the second type of garden waste remained in the step S4 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 450-480 ℃ at the temperature rise rate of 10-15 ℃ per min, and the pyrolysis device is kept for a second target time, so that the carbonization rate of the remained solid matters is 55-65%; |[0024] s6, mixing the solid matters obtained in the steps S3 and S5 according to the weight ratio of 1 (2-3) to obtain the carbon sink plant material for improving the planting soil. |[0025] The measurement of porosity and carbonization rate in the invention is a key factor for realizing the invention, and the measurement method is as follows:|[0026] The porosity is the percentage of the internal pore volume and the total volume of the material, and the total volume and the internal pore volume of the material need to be determined for measuring the porosity, specifically, the method comprises the steps of pumping air in carbonized leaves and trunks by means of vacuumizing, immersing the carbonized leaves or trunks in water under a vacuum state, releasing the vacuum, fully immersing the water in the pores of the material by soaking or boiling for about 1-3 h, enabling the water to be saturated and absorbed, and determining the water absorption capacity of the material by weighing the weight change before and after water absorption, so that the pore volume can be calculated. The whole material after water saturation is immersed in water, and the total volume of the material can be determined by measuring the change of the volume of the water. The method can relatively accurately measure the porosity of carbonized leaves or trunks. |[0027] The carbonization rate measuring method comprises the steps of carbonizing a sample material until the material weight is constant, wherein the carbonization rate of the material is regarded as 100%, comparing the weight of the material before and after the carbonization rate, dividing the weight loss part into 100 equal parts, and increasing the carbonization rate by 1% when the weight loss part is reduced by 1 part. For example, when 100 g of the trunk is carbonized to reach a constant weight of 45 g (in the present invention, the weight loss is determined to be constant by less than 5% of the sampling weight within 30 min), the weight loss is 55 g, and 55 g is divided into 100 equal parts, each part is 0.55 g, and when the weight obtained by weighing 100 g of the carbonized material is 78 g, the carbonization rate is= (78-45)/0.55 x 100% = 60%. The method can avoid errors generated by different sample materials and achieve relatively accurate measurement effect.|[0028] The following are comparison of the complete pyrolysis data of the tree leaves of the common tree species under the condition of the step S2 shown in the following table 1:|[0029] |[0030] the comparison of the complete pyrolysis data of the trunks of common tree species under the condition of the step S5 is shown in the following table 2: |[0031] |[0032] when the first type of garden waste is carbonized, the original structure is compact, the thick-wall cells are mainly, the cell gaps are less, the original macropores such as the guide pipe are mainly reserved after carbonization, and the newly generated micropores are less. When the carbonization rate of the first type of garden waste is 75-83% and the carbonization rate of the second type of garden waste is 55-65%, the index of the first type of garden waste and the index of complete carbonization are basically the same as the dominant pore type, the uniformity of pore distribution and the connectivity of pores except for the porosity. |[0033] The pore contrast index after carbonization of the first type of garden waste and the second type of garden waste is shown in the following table 3:|[0034] |[0035] The first type of incompletely carbonized garden waste (carbonization rate of 75-83%), the second type of incompletely carbonized garden waste (carbonization rate of 55-65%) were compared with the first type of completely carbonized garden waste and the second type of completely carbonized garden waste, and the comparison data are shown in table 4 below: |[0036] |[0037] Table 4 above shows that the incompletely carbonized first and second types of garden waste are different from the completely carbonized first and second types of garden waste in growth effect on microorganisms, and the root system of the plant needs the help of the microorganisms to absorb the nutrition position. |[0038] And 2022, taking campus fallen leaves and pruning trunks for experiments, wherein the campus tree species mainly comprise camphor, french phoenix tree and poplar, the weight ratio of the three tree species is 4:3:2, and the weight ratio of leaves to trunks is 1:2.5. And (3) taking the mixed leaves as first-class garden waste, taking the mixed trunk as second-class garden waste, and carbonizing.|[0039] The first type of incomplete carbonization garden waste (carbonization rate is 75-83%) and the second type of incomplete carbonization garden waste (carbonization rate is 55-65%) are degraded under natural conditions, and the comparison data are as follows:|[0040] TABLE 5 early stage (0-6 months) |[0041] |[0042] |[0043] TABLE 6 metaphase stage (6-18 months)|[0044] |[0045] TABLE 7 late stage (18 months or more)|[0046] |[0047] Tables 5-7 above show that in the degradation process, the pore changes of the first type of garden waste and the second type of garden waste are different, when the two are mixed in a weight ratio of 1:2.5, the two types of garden waste can keep enough pores for a long time, the number of mesopores and macropores is kept relatively stable, the ventilation, water retention and fertilizer retention of the planting soil can be kept, and a good living environment can be continuously provided for the growth of plants and soil microorganisms. The weight ratio of the growth amount of the leaves to the trunks in the natural growth state is about 1 (4-10), but the weight ratio of the leaves to the trunks after carbonization is 1 (2-3) when the branches which are normally pruned every year are relatively less, and the weight ratio of the leaves to the trunks is more consistent with the ratio of the actual fallen leaves to the pruned amount.|[0048] The first type of incompletely carbonized garden waste is degraded in the initial fast decomposing stage (0-6 months), and the residual organic matter is mainly decomposed, i.e. incompletely carbonized cellulose and hemicellulose are fast decomposed by microorganisms (such as fungi and bacteria) to release CO 2 and nutrients. The loss rate of organic carbon in the first type of garden waste partially carbonized can reach 40-60 percent. Pore structure change, namely micropores and mesopores formed by carbonization provide attachment sites for microorganisms and accelerate decomposition. And in the later stage of slow decomposition (more than 6 months), the main lignin is mainly decomposed, namely the residual lignin and carbonized carbon skeleton are slowly decomposed, and years or even longer are needed. The aromatic structure (e.g., graphitized carbon) formed during carbonization enhances resistance to decomposition, resulting in long-term carbon storage.|[0049] Table 8 is a comparison table of degradation data of the first type of garden waste at different carbonization rates:|[0050] |[0051] In Table 8, the carbonization rate of the first type of garden waste is preferably 75-83% in order to keep a larger porosity within 0-6 months, and the main reason is that the newly-formed pore channels continuously supplement the blocking of the pore channels, so that the porosity is maintained at a higher level for a long time, the first type of garden waste with low carbonization rate is fast degraded after 6 months, the porosity is also fast reduced, the first type of garden waste with high carbonization rate is basically in a continuously reduced state, and the carbonization rate is preferably 75-83% within 6 months, as a soil improvement plant material. |[0052] Table 9 is a comparison table of degradation data of the second type of garden waste at different carbonization rates:|[0053] |[0054] Table 9 shows that the carbonization rate of the second type of garden waste is preferably 55-65% in order to maintain the porosity substantially stable within 18 months, and that the porosity increases to higher and then decreases rapidly at 40% carbonization rate for 6 months, indicating that the degradation rate is too fast, and that the porosity continues to decrease over time, mainly due to biofilm attachment filling its pores, when the carbonization rate is 85-100%. |[0055] The first type of garden waste with carbonization rate of 75-83% and the second type of garden waste with carbonization rate of 55-65% are selected to be compounded, and the high porosity can be maintained for 0-18 months, wherein the new pore canal is mainly provided by the reduction of the first type of garden waste for 0-6 months, the high porosity is maintained, the first type of garden waste and the second type of garden waste are degraded together for 6-12 months, the high porosity is maintained, and the high porosity is maintained by the degradation of the second type of garden waste for 12-18 months.|[0056] When the planting soil is improved, the volume mixing ratio of the carbon sink plant material and the planting soil is (3-8): 1. The soil can be kept breathable for a long time at this ratio. Of course, other plants can be added during soil improvement. The first type of garden waste and the second type of garden waste are not easy to collapse in structure, high porosity can be maintained, long-acting water and fertilizer retention can be realized while carbon is collected and fixed, microorganism adhesion and growth can be facilitated, and activity of planting soil can be maintained. It can be used for improving garden soil and can be used for local material taking.|[0057] The invention is not limited to the above embodiments, and based on the technical solution disclosed in the invention, a person skilled in the art may make some substitutions and modifications to some technical features thereof without creative effort according to the technical content disclosed, and all the substitutions and modifications are within the protection scope of the invention. (CN120551173)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to a method for treating garden waste, in particular to a carbon sequestration method for garden waste and application of the method in soil improvement.|BACKGROUND ART|[0002] Since the content of CO 2 gas in nature is gradually increased due to the large-scale utilization of petroleum and coal, CO 2 is a greenhouse gas, and the content change in the atmosphere may have an adverse effect on the global environment, the concept of carbon sink, which generally refers to the process, activity and mechanism of removing carbon dioxide from the air, has been proposed in recent years. Carbon sink is a carbon deposit carrier in nature, and mainly utilizes photosynthesis of plants to absorb carbon dioxide in the atmosphere and fix the carbon dioxide in vegetation and soil through measures such as afforestation, forest management and vegetation restoration, so that the concentration of greenhouse gases in the atmosphere is reduced.|[0003] The existing garden waste mainly comprises leaves and branches which naturally wither and are manually pruned, and is natural substances, mainly comprises cellulose, lignin and the like, and in the nature, the leaves and branches are naturally decomposed by various bacteria and become CO 2 and H 2 O to enter natural circulation, so that a dynamic balance is formed, how to reduce the time of returning biological carbon fixation to the nature again or delay the time of returning the biological carbon fixation to the nature is reduced, and the concentration of greenhouse gases in the atmosphere can be kept to be relatively low in theory. Plants are carbonized, and can be kept for decades to thousands of years in nature, depending on the degree of carbonization.|[0004] The existing soil, especially clay, has low porosity, is easy to harden, is unfavorable for plant rooting and bacterial growth, and needs to be improved.|[0005] In the prior art, a method for improving soil by charcoal is reported, but the charcoal is mainly formed by insufficient combustion of main stems and branches of trees, has larger pores, low porosity compared with carbonized leaves, small total pore volume, smaller end points and fewer surface functional groups, so that the adsorption capacity of materials is weaker, the capacities of water retention, fertilizer retention and oxygen supply microorganisms are weaker, and an optimal soil improvement scheme cannot be provided. The simple tree leaves are carbonized, the porosity is higher, but the strength of the carbon skeleton is poor, and after the simple tree leaves are mixed with soil for improvement, the simple tree leaves are easy to generate structural damage and collapse of pores under the action of water, oxygen and microorganisms, so that the improved soil is disabled.|[0006] How to effectively fix carbon in garden waste and apply the carbon to soil improvement so that the soil can keep suitable plant and bacteria growth for a long time is a technical problem to be solved at present.|DISCLOSURE|Disclosure of Invention|[0007] The invention aims to provide a garden waste carbon sink sealing method for planting soil improvement, which can realize long-term carbon fixation, improve soil, enable planting soil to be breathable, retain water and fertilizer, and provide a good living environment for plant and soil microorganism growth.|[0008] The invention aims to realize the method for sealing and storing carbon sink of garden waste for improving planting soil, which comprises the following steps:|[0009] S1, collecting garden waste, carrying out rough separation and drying, combining roots, stems and leaves of herbaceous plants and leaves of woody plants into a first class, and combining the roots, branches and stems of the woody plants into a second class during rough separation, wherein the moisture content in the materials is lower than 15 percent; |[0010] S2, shredding the first type of garden waste treated in the step S1 to ensure that the average plane size is 6-10mm, stirring uniformly, sampling, weighing and pyrolyzing in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to ensure that the first type of garden waste is dehydrated, the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, the pyrolysis device is kept warm, meanwhile, the gas generated by pyrolysis is released, the liquid oil in the effluent product is led out, the rest solid matters are continuously weighed, when the constant weight of the pyrolyzed solid product lasts for 30min, stopping pyrolysis, recording the heat preservation time corresponding to the weight loss of the solid product, comparing the weight loss before and after carbonization of the material, equally dividing the weight loss into 100 parts, and regarding that the carbonization rate is increased by 1% for 1 part reduction, and determining the carbonization rate as a first target time; |[0011] S3, pyrolyzing the first type of garden waste remained in the step S2 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, then the pyrolysis device is kept at the temperature, and after the first target time, the carbonization rate of the remained solid matters is 75-83%; |[0012] S4, crushing the second type of garden waste after the step S1 into blocks with the maximum three-dimensional size of less than 3cm, sampling, weighing and pyrolyzing in an anaerobic environment, rapidly heating to 200 ℃ during pyrolysis, preserving heat for 15-20min to enable the blocks to lose water, slowly heating to 450-480 ℃ at the heating rate of 10-15 ℃ per min, preserving heat of a pyrolysis device, simultaneously releasing gas generated by pyrolysis of the blocks, introducing liquid oil in a product, continuously weighing the rest solid matters, stopping pyrolysis when the constant weight of the solid product after pyrolysis lasts for 30min, comparing the weights before and after carbonization of the material, equally dividing the weight loss part into 100 equal parts, and determining the carbonization rate as 1% for each 1% reduction and the carbonization rate as a second target time; |[0013] S5, pyrolyzing the second type of garden waste remained in the step S4 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 450-480 ℃ at the temperature rise rate of 10-15 ℃ per min, and the pyrolysis device is kept for a second target time, so that the carbonization rate of the remained solid matters is 55-65%; |[0014] s6, mixing the solid matters obtained in the steps S3 and S5 according to the weight ratio of 1 (2-3) to obtain the carbon sink plant material for improving the planting soil. |[0015] Further, in steps S2 and S4, it is determined that the weight loss of less than 5% of the sampled weight within 30 minutes is constant weight.|[0016] Further, in the case of improving the planting soil, the mixing ratio of the carbon sink plant material to the planting soil by volume is (3-8): 1.|[0017] Pyrolysis of plant biomass is a thermochemical process in which hemicellulose is first decomposed at a lower temperature, cellulose is decomposed in a medium temperature range, and lignin is finally decomposed at a higher temperature. The biological structure, chemical composition and physical characteristics of the tree leaf and the tree trunk are obviously different, the tree leaf is a leaf structure with parenchyma as a main part, and the tree trunk is a compact wood structure with a wood part as a main part, so that the carbonization process, the carbonization speed and the characteristic indexes of the tree trunk are obviously different. The leaves are pyrolyzed at a relatively low temperature, while the trunks are pyrolyzed at a relatively high temperature, so that the aim is to obtain a better carbon fixing effect, the yield of the biochar material is reduced due to the fact that the excessive pyrolysis temperature is increased, but the total structure of the biochar can be increased due to the fact that the pyrolysis temperature is increased, and therefore the specific surface area of the biochar is increased. The lower pyrolysis temperature can lead the biochar to have the characteristic of hydrophilicity. According to the invention, different pyrolysis temperatures are adopted for the first-class garden waste and the second-class garden waste, so that the aim is to ensure high-efficiency carbon fixation and reduce volatilization of oil and gas, and the organic matters are kept with more weight proportion of converted carbon as much as possible under the condition of fixed carbonization rate, thereby ensuring the carbon sink effect. Compared with the prior art, the invention has the beneficial effects that the roots, stems and leaves of herbaceous plants and the leaves of woody plants are combined into first-class garden waste, the carbonization rate is 75-83%, the roots, branches and stems of woody plants are combined into second-class garden waste, the carbonization rate is 55-65%, and carbonized products are mixed according to the weight ratio of 1 (2-3), so as to obtain the carbon sink plant material for planting soil improvement. The carbon sink plant material has good carbon fixing effect, so that the carbon sink plant material is not easy to degrade completely in nature, meanwhile, as the carbon sink plant material is not completely carbonized, part of lignin can be decomposed slowly, the self structure is not easy to collapse, high porosity is maintained, long-acting water and fertilizer retention can be realized, microorganism adhesion and growth can be facilitated, and the activity of planting soil can be maintained.|INVENTION MODE|Detailed Description|[0018] A garden waste carbon sink sealing method for planting soil improvement is carried out according to the following steps:|[0019] S1, collecting garden waste, carrying out rough separation and drying, combining roots, stems and leaves of herbaceous plants and leaves of woody plants into a first class during rough separation, combining the roots, branches and stems of woody plants into a second class, drying to ensure that the water content in the materials is lower than 15%, also discarding the herbaceous plants, only collecting the leaves as the first class of garden waste, taking the trunk as the second class of garden waste, classifying branches with diameters of more than 0.8cm into the second class of garden waste, and classifying branches with diameters of less than 0.8cm into the first class of garden waste. |[0020] S2, cutting the garden waste of the first type treated in the step S1 to ensure that the average plane size is 6-10mm, stirring uniformly, sampling, weighing and pyrolyzing in an anaerobic environment, wherein a reactor used for pyrolyzing is a fluidized bed, a fixed bed or a tubular furnace, heating to 200 ℃ rapidly during pyrolyzing, preserving heat for 15-20min to ensure that the water is lost, heating to 380-400 ℃ slowly at the heating rate of 10-15 ℃ per min, preserving heat of a pyrolyzing device, simultaneously releasing gas generated by pyrolysis, guiding liquid oil in a discharged product, continuously weighing the rest solid matters, stopping pyrolyzing when the constant weight of the pyrolyzed solid product is continuously maintained for 30min, recording the heat preservation time corresponding to the weight loss of the solid product, comparing the weight before and after carbonization of the material, dividing the weight loss into 100 equal parts, and determining that the carbonization rate is increased by 1% every 1% and the carbonization rate is 75-83% as a first target time;|[0021] S3, pyrolyzing the first type of garden waste remained in the step S2 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 380-400 ℃ at the temperature rise rate of 10-15 ℃ per min, then the pyrolysis device is kept at the temperature, and after the first target time, the carbonization rate of the remained solid matters is 75-83%; |[0022] S4, crushing the second type of garden waste after the step S1 into blocks with the largest three-dimensional size of less than 3cm, sampling, weighing and pyrolyzing in an anaerobic environment, wherein a reactor used for pyrolysis is a fluidized bed, a fixed bed or a tubular furnace, quickly heating to 200 ℃ during pyrolysis, preserving heat for 15-20min to enable the water to be lost, slowly heating to 450-480 ℃ at the heating rate of 10-15 ℃ per min, preserving heat of a pyrolysis device, simultaneously releasing gas generated by pyrolysis of the pyrolysis device, introducing liquid oil in a product, continuously weighing the rest solid matters, stopping pyrolysis when the constant weight of the solid product after pyrolysis lasts for 30min, comparing the weight of the material before and after carbonization, equally dividing the weight loss part into 100 equal parts, and determining that the carbonization rate is increased by 1% when the carbonization rate is reduced by 1%, and determining the carbonization rate as a second target time by 55-65%; |[0023] S5, pyrolyzing the second type of garden waste remained in the step S4 in an anaerobic environment, wherein the temperature is quickly raised to 200 ℃ during pyrolysis, the temperature is kept for 15-20min to enable the garden waste to lose water, then the temperature is slowly raised to 450-480 ℃ at the temperature rise rate of 10-15 ℃ per min, and the pyrolysis device is kept for a second target time, so that the carbonization rate of the remained solid matters is 55-65%; |[0024] s6, mixing the solid matters obtained in the steps S3 and S5 according to the weight ratio of 1 (2-3) to obtain the carbon sink plant material for improving the planting soil. |[0025] The measurement of porosity and carbonization rate in the invention is a key factor for realizing the invention, and the measurement method is as follows:|[0026] The porosity is the percentage of the internal pore volume and the total volume of the material, and the total volume and the internal pore volume of the material need to be determined for measuring the porosity, specifically, the method comprises the steps of pumping air in carbonized leaves and trunks by means of vacuumizing, immersing the carbonized leaves or trunks in water under a vacuum state, releasing the vacuum, fully immersing the water in the pores of the material by soaking or boiling for about 1-3 h, enabling the water to be saturated and absorbed, and determining the water absorption capacity of the material by weighing the weight change before and after water absorption, so that the pore volume can be calculated. The whole material after water saturation is immersed in water, and the total volume of the material can be determined by measuring the change of the volume of the water. The method can relatively accurately measure the porosity of carbonized leaves or trunks. |[0027] The carbonization rate measuring method comprises the steps of carbonizing a sample material until the material weight is constant, wherein the carbonization rate of the material is regarded as 100%, comparing the weight of the material before and after the carbonization rate, dividing the weight loss part into 100 equal parts, and increasing the carbonization rate by 1% when the weight loss part is reduced by 1 part. For example, when 100 g of the trunk is carbonized to reach a constant weight of 45 g (in the present invention, the weight loss is determined to be constant by less than 5% of the sampling weight within 30 min), the weight loss is 55 g, and 55 g is divided into 100 equal parts, each part is 0.55 g, and when the weight obtained by weighing 100 g of the carbonized material is 78 g, the carbonization rate is= (78-45)/0.55 x 100% = 60%. The method can avoid errors generated by different sample materials and achieve relatively accurate measurement effect.|[0028] The following are comparison of the complete pyrolysis data of the tree leaves of the common tree species under the condition of the step S2 shown in the following table 1:|[0029] |[0030] the comparison of the complete pyrolysis data of the trunks of common tree species under the condition of the step S5 is shown in the following table 2: |[0031] |[0032] when the first type of garden waste is carbonized, the original structure is compact, the thick-wall cells are mainly, the cell gaps are less, the original macropores such as the guide pipe are mainly reserved after carbonization, and the newly generated micropores are less. When the carbonization rate of the first type of garden waste is 75-83% and the carbonization rate of the second type of garden waste is 55-65%, the index of the first type of garden waste and the index of complete carbonization are basically the same as the dominant pore type, the uniformity of pore distribution and the connectivity of pores except for the porosity. |[0033] The pore contrast index after carbonization of the first type of garden waste and the second type of garden waste is shown in the following table 3:|[0034] |[0035] The first type of incompletely carbonized garden waste (carbonization rate of 75-83%), the second type of incompletely carbonized garden waste (carbonization rate of 55-65%) were compared with the first type of completely carbonized garden waste and the second type of completely carbonized garden waste, and the comparison data are shown in table 4 below: |[0036] |[0037] Table 4 above shows that the incompletely carbonized first and second types of garden waste are different from the completely carbonized first and second types of garden waste in growth effect on microorganisms, and the root system of the plant needs the help of the microorganisms to absorb the nutrition position. |[0038] And 2022, taking campus fallen leaves and pruning trunks for experiments, wherein the campus tree species mainly comprise camphor, french phoenix tree and poplar, the weight ratio of the three tree species is 4:3:2, and the weight ratio of leaves to trunks is 1:2.5. And (3) taking the mixed leaves as first-class garden waste, taking the mixed trunk as second-class garden waste, and carbonizing.|[0039] The first type of incomplete carbonization garden waste (carbonization rate is 75-83%) and the second type of incomplete carbonization garden waste (carbonization rate is 55-65%) are degraded under natural conditions, and the comparison data are as follows:|[0040] TABLE 5 early stage (0-6 months) |[0041] |[0042] |[0043] TABLE 6 metaphase stage (6-18 months)|[0044] |[0045] TABLE 7 late stage (18 months or more)|[0046] |[0047] Tables 5-7 above show that in the degradation process, the pore changes of the first type of garden waste and the second type of garden waste are different, when the two are mixed in a weight ratio of 1:2.5, the two types of garden waste can keep enough pores for a long time, the number of mesopores and macropores is kept relatively stable, the ventilation, water retention and fertilizer retention of the planting soil can be kept, and a good living environment can be continuously provided for the growth of plants and soil microorganisms. The weight ratio of the growth amount of the leaves to the trunks in the natural growth state is about 1 (4-10), but the weight ratio of the leaves to the trunks after carbonization is 1 (2-3) when the branches which are normally pruned every year are relatively less, and the weight ratio of the leaves to the trunks is more consistent with the ratio of the actual fallen leaves to the pruned amount.|[0048] The first type of incompletely carbonized garden waste is degraded in the initial fast decomposing stage (0-6 months), and the residual organic matter is mainly decomposed, i.e. incompletely carbonized cellulose and hemicellulose are fast decomposed by microorganisms (such as fungi and bacteria) to release CO 2 and nutrients. The loss rate of organic carbon in the first type of garden waste partially carbonized can reach 40-60 percent. Pore structure change, namely micropores and mesopores formed by carbonization provide attachment sites for microorganisms and accelerate decomposition. And in the later stage of slow decomposition (more than 6 months), the main lignin is mainly decomposed, namely the residual lignin and carbonized carbon skeleton are slowly decomposed, and years or even longer are needed. The aromatic structure (e.g., graphitized carbon) formed during carbonization enhances resistance to decomposition, resulting in long-term carbon storage.|[0049] Table 8 is a comparison table of degradation data of the first type of garden waste at different carbonization rates:|[0050] |[0051] In Table 8, the carbonization rate of the first type of garden waste is preferably 75-83% in order to keep a larger porosity within 0-6 months, and the main reason is that the newly-formed pore channels continuously supplement the blocking of the pore channels, so that the porosity is maintained at a higher level for a long time, the first type of garden waste with low carbonization rate is fast degraded after 6 months, the porosity is also fast reduced, the first type of garden waste with high carbonization rate is basically in a continuously reduced state, and the carbonization rate is preferably 75-83% within 6 months, as a soil improvement plant material. |[0052] Table 9 is a comparison table of degradation data of the second type of garden waste at different carbonization rates:|[0053] |[0054] Table 9 shows that the carbonization rate of the second type of garden waste is preferably 55-65% in order to maintain the porosity substantially stable within 18 months, and that the porosity increases to higher and then decreases rapidly at 40% carbonization rate for 6 months, indicating that the degradation rate is too fast, and that the porosity continues to decrease over time, mainly due to biofilm attachment filling its pores, when the carbonization rate is 85-100%. |[0055] The first type of garden waste with carbonization rate of 75-83% and the second type of garden waste with carbonization rate of 55-65% are selected to be compounded, and the high porosity can be maintained for 0-18 months, wherein the new pore canal is mainly provided by the reduction of the first type of garden waste for 0-6 months, the high porosity is maintained, the first type of garden waste and the second type of garden waste are degraded together for 6-12 months, the high porosity is maintained, and the high porosity is maintained by the degradation of the second type of garden waste for 12-18 months.|[0056] When the planting soil is improved, the volume mixing ratio of the carbon sink plant material and the planting soil is (3-8): 1. The soil can be kept breathable for a long time at this ratio. Of course, other plants can be added during soil improvement. The first type of garden waste and the second type of garden waste are not easy to collapse in structure, high porosity can be maintained, long-acting water and fertilizer retention can be realized while carbon is collected and fixed, microorganism adhesion and growth can be facilitated, and activity of planting soil can be maintained. It can be used for improving garden soil and can be used for local material taking.|[0057] The invention is not limited to the above embodiments, and based on the technical solution disclosed in the invention, a person skilled in the art may make some substitutions and modifications to some technical features thereof without creative effort according to the technical content disclosed, and all the substitutions and modifications are within the protection scope of the invention. Family Number|(115814465)|115814465|Abstract|(CN120551173 A)|The invention discloses a garden waste carbon sequestration and storage method for improving planting soil , which comprises the following steps : collecting , classifying and crushing garden wastes , classifying different collected objects , carrying out incomplete carbonization treatment , merging roots , stems and leaves of herbaceous plants and leaves of woody plants into a first type of garden wastes , and ensuring that the carbonization rate is 75-83% ; roots , branches and stems of woody plants are combined into second - class garden waste , and the carbonization rate is 55-65% ; and mixing carbonized products according to a weight ratio of 1 : ( 2-3 ) to obtain the carbon sequestration plant material for improving the planting soil . The carbon sequestration planting material has a good carbon sequestration effect , so that the carbon sequestration planting material is not easily and completely degraded in nature , meanwhile , due to the fact that the carbon sequestration planting material is not completely carbonized , part of lignin can be retained and can be slowly decomposed , the self structure is not easily collapsed , high porosity is maintained , long - acting water retention and fertilizer retention can be achieved , meanwhile , attachment growth of microorganisms can be facilitated , and the vitality of planting soil is kept . |CPC codes|(CN120551173 A)|A01B - 079/00 |IPC codes|(CN120551173 A)|A01B - 079/00 | Environmental technology|Other special machines A01B-079/00|B09B-003/00|B09B-003/00/83|C05D-009/00|C05D-009/02|C05F-011/00|C05G-003/80|Y02E-050/10|Y02E-050/30|Y02W-030/43|Y02W-030/47 A01B-079/00|B09B-003/00|B09B-003/00/83|C05D-009/00|C05D-009/02|C05F-011/00|C05G-003/80|Y02E-050/10|Y02E-050/30|Y02W-030/43|Y02W-030/47 A01B-079/00|B09B-003/35|B09B-003/40|B09B-101/85 A01B-079/00|B09B-003/35|B09B-003/40|B09B-101/85 PENDING (CN120551173)|PENDING ALIVE (CN120551173)|ALIVE (CN120551173)|LEGAL DETAILS FOR CN120551173|Actual or expected expiration date=2045-07-08|Legal state=ALIVE|Status=PENDING|Event publication date=2025-07-08|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510936450|Application date=2025-07-08|Standardized application number=2025CN-0936450|Event publication date=2025-08-29|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120551173|Publication stage code=A|Publication date=2025-08-29|Standardized publication number=CN120551173|Event publication date=2025-08-29|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-09-16|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN120551173)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKdFwM8ubTFzRlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000078770533&ekey=2338&xpn=CN120551173&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=XGRvysjX9nBcSEWC0cKz1pNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN120551173)|CN (CN120551173)|NAME=YANGZHOU POLYTECHNIC INSTITUTE , COUNTRY=CN (CN120551173)|NAME=DONG XUDONG;NANJING SUKE INTELLECTUAL PROPERTY AGENT. LTD. , REG=32102 (CN120551173)|CN (CN120551173)|NAME=YU JINGJING, COUNTRY=CN 0 1 Titre: (CN120551173)|Garden waste carbon sink storage method for improving planting soil Résumé: (CN120551173)|The invention discloses a garden waste carbon sequestration and storage method for improving planting soil, which comprises the following steps: collecting, classifying and crushing garden wastes, classifying different collected objects, carrying out incomplete carbonization treatment, merging roots, stems and leaves of herbaceous plants and leaves of woody plants into a first type of garden wastes, and ensuring that the carbonization rate is 75-83%; roots, branches and stems of woody plants are combined into second-class garden waste, and the carbonization rate is 55-65%; and mixing carbonized products according to a weight ratio of 1: (2-3) to obtain the carbon sequestration plant material for improving the planting soil. The carbon sequestration planting material has a good carbon sequestration effect, so that the carbon sequestration planting material is not easily and completely degraded in nature, meanwhile, due to the fact that the carbon sequestration planting material is not completely carbonized, part of lignin can be retained and can be slowly decomposed, the self structure is not easily collapsed, high porosity is maintained, long-acting water retention and fertilizer retention can be achieved, meanwhile, attachment growth of microorganisms can be facilitated, and the vitality of planting soil is kept. 68 Abstract gpt-4o-mini no The article focuses on a method for carbon sequestration using garden waste and does not involve the accelerated weathering of minerals or CO₂ capture through mineral carbonation.
70 CN202211664591 CN202211664591 CN115852159 104319154 CN115852159 A 2023-03-28 [CN115852159] 2022-12-23 2022-12-23 2023-03-28 (CN115852159)|2025-12-02 (CN115852159)|Method for recovering gold in carbon-gold catalyst (CN115852159)|The invention discloses a method for recovering gold in a carbon-gold catalyst. The method comprises the following steps: S1, crushing a waste Au/C catalyst; s2, soaking the Au/C catalyst in concentrated sulfuric acid for primary carbon removal; s3, washing the Au/C catalyst subjected to primary carbon removal with concentrated nitric acid, and removing concentrated sulfuric acid on the surface of a solid while secondary carbon removal; s4, the solid obtained in S3 is soaked in aqua regia to dissolve Au and residual carbon surrounded by Au, Au and aqua regia react to generate H [AuCl4], and the carbon reaction is gas recovery; s5, heating and evaporating the solution obtained in the step S4, and evaporating residual HNO3 and HCl to obtain gold trichloride; s6, a reducing agent is added into the gold trichloride, and spongy crude gold is obtained through reduction; s7, purifying the crude gold obtained in the step S6 to obtain a pure gold block; while the gold is mildly recovered, the substance participating in the recovery can be recycled to form a closed loop, so that the effective acid concentration for dissolving the gold is guaranteed, and the recovery of the noble metal is promoted. ZHEJIANG SHENGYANG RENEWABLE RESOURCES TECHNOLOGY (CN115852159)|Zhejiang Shengyang Renewable Resources Technology Co.,Ltd. ([CN]) XU YIZHEN|ZHANG JIANPING|ZHOU SHUIJUN|XU SHENGYANG|YANG ZHANGBAO (CN115852159)|XU YIZHEN|ZHANG JIANPING|ZHOU SHUIJUN|XU SHENGYANG|YANG ZHANGBAO (CN115852159)|HU ENHAN;JINHUA WUSHI PATENT AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 33340 (CN115852159)|However, gold, as a noble metal, is expensive, resulting in a high cost of gold-carbon catalyst, which should be efficiently recovered.|The invention adopts the showering nitric acid, on one hand, the concentration of the concentrated nitric acid is ensured to be high enough; the method avoids the problems that the effective collision of nitrate radicals and carbon-containing substances is less due to insufficient concentration of nitric acid, and the thorough removal of the carbon-containing substances cannot be ensured; on the other hand, concentrated nitric acid is unstable and has chemical reaction when meeting light, the concentration is too high, the concentrated nitric acid is easy to volatilize and decompose, the production condition is too harsh, and light shielding or matching is needed, so that the concentrated nitric acid effectively ensures the flow of the concentrated nitric acid relative to solid matters to promote the decomposition of carbon in the solid matters by spraying, and the solid matters are fully covered by the fluidity of liquid to form effective contact of the solid phases and the liquid phases.| (CN115852159)|1. A method for recovering gold from a carbon gold catalyst is characterized by comprising the following steps:the method comprises the following steps:s1, crushing a waste Au/C catalyst, wherein the particle size of the crushed waste Au/C catalyst is 5-15 microns;s2, soaking the Au/C catalyst in concentrated sulfuric acid for primary decarbonization;the process conditions for the primary carbon removal are as follows:heating concentrated sulfuric acid to 80-100 ℃;adding Au/C powder into the heated concentrated sulfuric acid;stirring and reacting for 20-40 min;recovering the generated sulfur dioxide;filtering the solid;s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the solid surface while performing secondary decarbonization;s4, soaking the solid of the S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, and reacting Au with the aqua regia to generate H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;s5, heating and evaporating the solution obtained in the S4, and evaporating the residual HNO 3 And HCl to obtain gold trichloride;s6, adding a reducing agent into the gold trichloride, and reducing to obtain spongy crude gold;and S7, purifying the crude gold obtained in the S6 to obtain pure gold blocks.| (CN115852159)|The invention aims to provide a method for recovering gold in a carbon gold catalyst, which can be used for recycling substances participating in recovery to form a closed loop while recovering gold mildly, so that the effective acid concentration of gold dissolution is ensured, and the recovery of precious metals is promoted.|The invention discloses a method for recovering gold in a carbon gold catalyst, which comprises the following steps: s1, crushing a waste Au/C catalyst; s2, soaking the Au/C catalyst in concentrated sulfuric acid for primary decarbonization; s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization; s4, soaking the solid of the S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, and reacting Au with the aqua regia to generate H [ AuCl ] 4 ]The carbon reaction is gas recovery; s5, heating and evaporating the solution obtained in the S4, and evaporating the residual HNO 3 And HCl to obtain gold trichloride; s6, adding a reducing agent into the gold trichloride, and reducing to obtain spongy crude gold; s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks; the invention recovers gold at moderate temperatureMeanwhile, the substances participating in recovery can be recycled to form a closed loop, so that the effective acid concentration of gold dissolution is ensured, and the recovery of precious metals is promoted. The invention relates to a precious metal recovery technology, in particular to a mild method for recovering gold from carbon gold.| (CN115852159)|RECOVERING GOLD(100,13)|CARBON GOLD(100,12)|CARBON GOLD CATALYST(100,11)|GOLD DISSOLUTION ACID(79,2)|NITRATE RADICAL COLLISION(78,1)|SPONGY CRUDE GOLD(70,7)|PRIMARY DECARBONIZATION(68,11)|CONCENTRATED NITRIC ACID(57,22)|GOLD DISSOLUTION(54,3)|RECYCLING(52,15)|RESIDUAL HNO(52,7)|DISSOLVE AU(49,6)|CONCENTRATED SULFURIC ACID(47,52)|DECARBONIZATION(46,9)|SPONGE CRUDE GOLD(45,1)|CRUDE GOLD(44,9)|GOLD TRICHLORIDE(43,19)|AQUA REGIA(39,27)|SHOWERING NITRIC ACID(38,1)|SOLID MATTER(37,3)|NITRATE RADICAL(36,2)|NITRIC ACID(33,57)|ALKALI LIQUOR ADJUSTING SUBSTANCE(32,2)|GOLD BLOCK(30,10)|RESIDUAL CARBON(29,10)|SULFURIC ACID(27,74)|RECOVERING GAS(26,1)|LIGHT SHIELDING(25,1)|AU C CATALYST(24,19)|MAGNETIC CRUCIBLE(24,7)|RECOVERING PRECIOUS METAL(24,1)|GOLD MUD(23,7)|HEATED CONCENTRATED SULFURIC ACID(23,2)|MIXING HAUCL(23,2)|AUCL(22,8)|NITROGEN DIOXIDE RECOVERY(22,6)|SPRAYING(22,3)|AU ACCOUNT(22,2)|MODERATE(22,1)|ACTIVE INGREDIENT(21,2)|SPONGE ROUGH GOLD(20,5)|GOLD CARBON CATALYST(20,2)|PRODUCTION CONDITION(19,1)|SULFUR DIOXIDE(18,7)|GOLD TRICHLORIDE REDUCTION(18,2)|SOLID PHASE(17,1)|GENERATED SULFUR DIOXIDE(16,3)|NITROGEN DIOXIDE(15,14)|HCL(15,7)|SULFUROUS ACID(15,4)|PRECIOUS METAL(15,3)|SMELTING(14,3)|GOLD(13,16)|WASTE AU C CATALYST(13,10)|HYDROCHLORIC ACID(12,12)|PROCESS CONDITION(12,6)|CLOSED LOOP(12,3)|INTRODUCTION(12,3)|STANDING(12,2)|CARBON REACTION(11,7)|REDUCING AGENT(11,7)|BORAX MASS(11,4)|PRIMARY CARBON REMOVAL(11,3)|NOBLE METAL(11,1)|SPENT CATALYST PURCHASE TON(11,1)|CHLOROAURIC ACID(10,5)|HYDRAZINE STOICHIOMETRIC RATIO(10,5)|DISSOLVING GOLD(10,3)|S12(10,2)|CHEMICAL REACTION(10,1)|CARBON DIOXIDE(9,8)|RECOVERY PROFIT(9,2)|WASTE CATALYST PARTICLE(9,2)|SIMULATED DEACTIVATED CATALYST(9,1)|SPONGE COARSE GOLD(9,1)|INORGANIC CARBON(8,6)|ADDING AU C(8,2)|DISSOLVING AU(8,2)|HYDRAZINE PARTICIPATION(8,1)|MASS VOLUME RATIO(8,1)|RECYCLING PROFIT(8,1)|AU C CATALYST MASS(7,2)|GOLD RECOVERY(7,2)|LIQUID PHASE(7,2)|PURIFICATION PROCESS CONDITION(7,2)|RESIDUAL NITROGEN GAS(7,2)|AQUA REGIA CONSUMPTION(7,1)|AU DISSOLUTION(7,1)|CATALYST CAKING(7,1)|PARTICLE SIZE(6,6)|REMOVING CARBON(6,6)|CATALYST RESIDUE(6,2)|ACTIVE CARBON(5,5)|ARTIFICIAL RECOVERY(5,1)|AU PARTICLE(5,1)|AU RECOVERY(5,1)|CRUSHED PARTICLE(5,1)|POWDER CALCINATION(5,1)|REACTANT COVERING(5,1)|RECOVERED CATALYST(5,1)|SUBSTANCE GOLD PARTICLE(5,1)|BALL MILLING(4,4)|CRUSHED AU C CATALYST(4,4)|GENERATED NITROGEN DIOXIDE(4,4)|REDUCING AGENT HYDRAZINE(4,4)|SOLID MASS VOLUME(4,4)|SULFURIC ACID VOLUME(4,4)|VOLUME MASS(4,4)|ALDEHYDE(4,2)|CARBON CARRIER(4,2)|REACTION TANK(4,2)|RECOVERY COST(4,2)|ACTIVATED CARBON ADSORBABILITY(4,1)|AU REDUCTION(4,1)|CATALYTIC PERFORMANCE(4,1)|DISSOLVE CARBON(4,1)|ELECTRICITY CHARGE(4,1)|ELECTRONEGATIVITY(4,1)|GOLD CARBON CATALYST HIGH COST(4,1)|KINGSOAKING(4,1)|LABOR CHARGE(4,1)|OXIDABILITY(4,1)|OXIDIZABILITY(4,1)| (CN115852159)|1. A method for recovering gold from a carbon gold catalyst is characterized by comprising the following steps:|the method comprises the following steps:|s1, crushing a waste Au/C catalyst, wherein the particle size of the crushed waste Au/C catalyst is 5-15 microns;|s2, soaking the Au/C catalyst in concentrated sulfuric acid for primary decarbonization;|the process conditions for the primary carbon removal are as follows:|heating concentrated sulfuric acid to 80-100 ℃;|adding Au/C powder into the heated concentrated sulfuric acid;|stirring and reacting for 20-40 min;|recovering the generated sulfur dioxide;|filtering the solid;|s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the solid surface while performing secondary decarbonization;|s4, soaking the solid of the S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, and reacting Au with the aqua regia to generate H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|s5, heating and evaporating the solution obtained in the S4, and evaporating the residual HNO 3 And HCl to obtain gold trichloride;|s6, adding a reducing agent into the gold trichloride, and reducing to obtain spongy crude gold;|and S7, purifying the crude gold obtained in the S6 to obtain pure gold blocks.|2. The recycling method according to claim 1, characterized in that: the process conditions for recovering the sulfur dioxide in the S2 are as follows:|introducing water to form sulfurous acid, and introducing oxygen into the sulfurous acid to obtain sulfuric acid;|heating and concentrating sulfuric acid to obtain concentrated sulfuric acid, and introducing the concentrated sulfuric acid into S2 for recycling.|3. A recycling method according to claim 1, characterized in that: the process conditions for recovering the nitric oxide and the nitrogen dioxide generated by the S3 and the S4 are as follows:|introducing water and oxygen into the residual nitrogen-containing gas for many times to convert the nitrogen-containing gas into nitric acid;|heating and concentrating nitric acid to obtain concentrated nitric acid, and adding the concentrated nitric acid into S3 for recycling.|4. A recycling method according to claim 1, characterized in that: the specific manner of reduction of gold trichloride in S6 is as follows: dissolving gold trichloride and hydrazine in hydrochloric acid, and reacting chloroauric acid with hydrochloric acid to form HAuCl 4 Hydrazine with hydrochloric acid to form N 2 H 5 Cl, reduction reaction as follows:|3N 2 H 5 Cl+4HAuCl 4 →3N 2 +4Au+19HCl。|5. a recycling method according to claim 1, characterized in that: the purification process conditions in S7 comprise the following steps:|s71, washing the sponge crude gold with nitric acid, filtering, cleaning and drying;|s72, putting the gold mud into a magnetic crucible, adding 10-15 wt% of borax, and smelting into pure gold blocks at 1000-1100 ℃.|6. A recycling method according to any one of claims 1 to 5, characterized in that: the concentrated sulfuric acid concentration for the first decarbonization in the S2 is 9.2mo1/L to 16mol/L.|7. The recovery process according to any one of claims 1 to 5, characterized in that: the mass-volume ratio of the Au/C powder to the concentrated sulfuric acid is (20 g to 40 g): 1L of the total amount of the active ingredients.|8. The recovery process according to any one of claims 1 to 5, characterized in that: the concentration of the concentrated nitric acid for spraying and washing the solid in the S2 in the S3 is 14mol/L to 17mol/L.|9. A recycling method according to claim 1, characterized in that: the mass of the Au/C catalyst to be recovered is calculated according to 100 parts, wherein Au accounts for 10-30 parts, and the balance is carbon.|10. A recycling method according to claim 9, characterized in that: the preparation method of the Au/C catalyst comprises the following steps:|s11, mixing HAuCl 4 Mixing the solution and the active carbon dispersed by using the alkali liquor according to the mass part ratio, and uniformly stirring;|wherein the adjusting substance of the alkali liquor is NaHCO 3 ;|S12, continuously stirring; standing; and filtering, reducing and drying to obtain the Au/C catalyst. (CN115852159)|TECHNICAL FIELD|[0001] The invention relates to a precious metal recovery technology, in particular to a mild method for recovering gold from carbon gold.|BACKGROUND ART|[0002] The carbon-supported gold is widely applied to the production of chemical products, such as the catalytic combustion of hydrocarbons, water gas conversion, liquid-phase chemical oxidation reaction and the like, and effectively improves the reaction rate and degree. The invention patents of CN105107498B and CN112156809A both describe the preparation method of carbon-supported gold catalyst, but as the catalyst, the reaction temperature is too high along with the prolonging of the service time, and agglomeration is generated; or the surface cannot be removed in time because of excessive covering of reactants or products; the catalytic efficiency will gradually decrease to a point of failure and be discarded. However, gold, as a noble metal, is expensive, resulting in a high cost of gold-carbon catalyst, which should be efficiently recovered.|[0003] The common method in the existing technical scheme aiming at gold recovery is to calcine at high temperature to remove carbon, the high-temperature carbon removal process has large energy consumption and causes high recovery cost, and in the calcination process, part of carbon carriers are not removed completely because the temperature is less than 1000 ℃; the residual carbon is contacted with oxidizing acid capable of dissolving gold in the soaking process, and the carbon carrier reacts with the oxidizing acid to dilute the concentration of the oxidizing acid, so that the dissolution of gold is influenced, and the recovery of precious metals is not facilitated.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a method for recovering gold in a carbon gold catalyst, which can be used for recycling substances participating in recovery to form a closed loop while recovering gold mildly, so that the effective acid concentration of gold dissolution is ensured, and the recovery of precious metals is promoted.|[0005] In order to solve the technical problem, the technical scheme of the invention is as follows: a method for recovering gold in a carbon gold catalyst comprises the following steps:|[0006] s1, crushing the waste Au/C catalyst, wherein the particle size is 5-15 mu m after crushing;|[0007] s2, soaking the Au/C catalyst in concentrated sulfuric acid for primary decarbonization;|[0008] the process conditions for the primary carbon removal are as follows:|[0009] heating concentrated sulfuric acid to 80-100 ℃;|[0010] adding Au/C powder into the heated concentrated sulfuric acid;|[0011] stirring and reacting for 20-40 min;|[0012] recovering the generated sulfur dioxide;|[0013] filtering the solid;|[0014] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0015] s4, soaking the solid of the S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, and reacting Au with the aqua regia to generate H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0016] s5, heating and evaporating the solution obtained in the S4, and evaporating the residual HNO 3 And HCl to obtain gold trichloride;|[0017] s6, adding a reducing agent into the gold trichloride, and reducing to obtain spongy crude gold;|[0018] and S7, purifying the crude gold obtained in the S6 to obtain pure gold blocks.|[0019] The preferred process conditions for sulfur dioxide recovery in S2 are as follows:|[0020] introducing water to form sulfurous acid, and introducing oxygen into the sulfurous acid to obtain sulfuric acid;|[0021] the reaction principle is as follows:|[0022] 2H 2 SO 3 +O 2 →2H 2 SO 4|[0023] heating and concentrating sulfuric acid to obtain concentrated sulfuric acid, and introducing the concentrated sulfuric acid into S2 for recycling.|[0024] The preferred process conditions for the recovery of nitric oxide and nitrogen dioxide produced by S3 and S4 are as follows:|[0025] introducing water and oxygen into the residual nitrogen-containing gas for many times to convert the nitrogen-containing gas into nitric acid;|[0026] the reaction principle is as follows:|[0027] 3NO 2 +H 2 O→2HNO 3 +NO;|[0028] 2NO+O 2 →2NO 2 ;|[0029] heating and concentrating nitric acid to obtain concentrated nitric acid, and adding the concentrated nitric acid into S3 for recycling.|[0030] The preferable specific manner of reduction of gold trichloride in S6 is as follows: dissolving gold trichloride and hydrazine in hydrochloric acid, and forming HAuCl by chloroauric acid and hydrochloric acid 4 Hydrazine with hydrochloric acid to form N 2 H 5 Cl, reduction reaction as follows:|[0031] 3N 2 H 5 Cl+4HAuCl 4 →3N 2 +4Au +19HCl. The invention reduces the gold in the chloroauric acid to the simple substance gold particles for dissolving out, and obtains the crude gold filled with sponge.|[0032] Preferably, the purification process conditions in S7 include the following steps:|[0033] s71, washing the sponge coarse gold with nitric acid, filtering, cleaning and drying;|[0034] s72, putting the gold mud into a magnetic crucible, adding 10-15 wt% of borax, and smelting into pure gold blocks at 1000-1100 ℃.|[0035] Preferably, the concentrated sulfuric acid concentration for the first carbon removal in S2 is 9.2mo1/L to 16mol/L.|[0036] The mass volume ratio of the Au/C powder to the concentrated sulfuric acid is preferably (20 g to 40 g): 1L of the total amount of the active ingredients. The invention adopts the showering nitric acid, on one hand, the concentration of the concentrated nitric acid is ensured to be high enough; the method avoids the problems that the effective collision of nitrate radicals and carbon-containing substances is less due to insufficient concentration of nitric acid, and the thorough removal of the carbon-containing substances cannot be ensured; on the other hand, concentrated nitric acid is unstable and has chemical reaction when meeting light, the concentration is too high, the concentrated nitric acid is easy to volatilize and decompose, the production condition is too harsh, and light shielding or matching is needed, so that the concentrated nitric acid effectively ensures the flow of the concentrated nitric acid relative to solid matters to promote the decomposition of carbon in the solid matters by spraying, and the solid matters are fully covered by the fluidity of liquid to form effective contact of the solid phases and the liquid phases.|[0037] Preferably, the concentration of the concentrated nitric acid for spraying and washing the solid in the S2 in the S3 is 14mol/L to 17mol/L. Concentrated sulfuric acid which is used for primary carbon removal and can not further dissolve carbon is remained in the solid, and is not beneficial to hydrazine participation in reduction, so that when nitric acid is used for washing, sulfuric acid with lower concentration has weak reaction capacity with carbon, N has stronger electronegativity than S, concentrated nitric acid is easier to react with carbon, when nitric acid is sprayed and washed, nitrate radicals react with carbon-containing substances in preference to remove carbon for the second time, sulfate radicals in the system flow away along with unreacted nitric acid, and residual sulfuric acid is effectively removed.|[0038] Preferably, the mass of the Au/C catalyst to be recovered accounts for 100 parts, wherein Au accounts for 10-30 parts, and the balance is carbon.|[0039] The preferred preparation method of the Au/C catalyst comprises the following steps:|[0040] s11, mixing HAuCl 4 Mixing the solution and the active carbon dispersed by using alkali liquor according to the mass part ratio, and uniformly stirring;|[0041] wherein the adjusting substance of the alkali liquor is NaHCO 3 ;|[0042] S12, continuously stirring; standing; and filtering, reducing and drying to obtain the Au/C catalyst.|[0043] By adopting the technical scheme, the invention has the beneficial effects that:|[0044] the main reason for the inactivation of the Au/C catalyst is that the surface of the catalyst is coated by carbon-containing organic matters such as aldehydes and acids, so that the catalyst cannot generate a catalytic action, and the carbon-containing organic matters also exist in the catalyst to be recovered; the caking of the catalyst can be caused in the using process, and the catalytic performance is further reduced; the invention crushes the carbon with organic matter as load and the gold particles with catalytic activity, firstly, the concentrated sulfuric acid is used for soaking under heating condition, the concentrated sulfuric acid has strong dehydration and oxidation effects, can convert the carbon-containing organic matter into carbon dioxide and water, and can also generate the carbon dioxide and the water by dissolving the carrier carbon material with the concentrated sulfuric acid; because the mass ratio of organic carbon to inorganic carbon in the waste catalyst particles is high, the organic carbon and the inorganic carbon are removed by soaking in concentrated sulfuric acid, and the waste catalyst particles are further crushed by using a chemical reaction consumption mode; the specific reaction mode is as follows:|[0045] C+2H 2 SO 4 (concentrated) → CO 2 ↑+2SO 2 ↑+2H 2 O;|[0046] The concentrated sulfuric acid selectively consumes carbon materials in the catalyst compound under the heating condition, the crushed particle structure of the Au/C catalyst is decomposed and broken in the process, and a certain amount of sulfuric acid which is not enough to dissolve organic carbon and inorganic carbon is adsorbed in the activated carbon due to the adsorbability of the activated carbon;|[0047] after the waste catalyst is subjected to primary decarbonization, the rest part of the active carbon further limits the decarbonization due to the adsorption of sulfonic acid groups and the reduction of the concentration of concentrated sulfuric acid;|[0048] then, concentrated nitric acid is used for washing Au/C catalyst particles which are subjected to preliminary carbon removal and crushing by concentrated sulfuric acid, and after organic carbon on the surfaces of the catalyst particles is removed, the active carbon connected with Au is further subjected to oxidation reduction by utilizing stronger oxidizability of the concentrated nitric acid to remove the active carbon; a large amount of concentrated sulfuric acid and concentrated nitric acid are used for consuming carbon in the waste catalyst, and aqua regia for dissolving Au is guaranteed to have stable concentration, so that Au and residual carbon are quickly dissolved;|[0049] the concentrated sulfuric acid is removed in the concentrated nitric acid spraying process, simultaneously, carbon materials in Au/C catalyst particles are thoroughly and selectively removed, and the Au/C catalyst particles with smaller sizes are obtained, and the specific reaction principle is as follows:|[0050] C+4HNO 3 (concentrated) → CO 2 ↑+4NO 2 ↑+2H 2 O;|[0051] The concentrated sulfuric acid which is used for removing carbon twice and can remove the concentrated sulfuric acid which is remained after the carbon is removed once, and the sulfuric acid reacts with hydrazine to obtain N 2 H 4 +H 2 SO 4 →N 2 H 6 SO 4 Not beneficial to the effective reduction of Au;|[0052] the Au particles which are crushed by concentrated sulfuric acid and concentrated nitric acid and are decarbonized and still contain a certain amount of residual carbon are immersed in aqua regia to obtain chloroauric acid, and the reaction mechanism of Au and aqua regia is as follows:|[0053] Au+HNO 3 +4HCl→H[AuCl 4 ]+NO↑+2H 2 O;|[0054] heating and decomposing chloroauric acid to obtain AuCl 3 The specific principle is as follows:|[0055] H[AuCl 4 ]→HCl+AuCl 3 ;|[0056] then reducing and purifying to obtain pure gold;|[0057] aiming at the existence of a large amount of organic carbon and inorganic carbon in the waste Au/C catalyst, concentrated sulfuric acid is firstly used for removing carbon for the first time; then, carrying out secondary decarbonization by using concentrated nitric acid with higher oxidability; after most of carbon is removed, the aqua regia is used for effectively dissolving gold, so that the problems that the concentration of nitric acid and hydrochloric acid in the aqua regia is reduced due to the consumption of carbon materials, the dissolution of Au is slowed and incomplete, and the gold recovery is not facilitated due to the preferential reaction of the aqua regia with carbon materials caused by the existence of carbon when the gold is dissolved due to the existence of a large amount of organic carbon and inorganic carbon are avoided;|[0058] in the prior art, carbon is removed by calcination, and the acid substances are recycled by oxidation-reduction reaction in the process of removing the carbon; the invention utilizes the addition sequence of concentrated sulfuric acid, concentrated nitric acid and aqua regia to recover sulfur dioxide and nitrogen dioxide corresponding to the used concentrated sulfuric acid and concentrated nitric acid by oxidation reduction of organic carbon and inorganic carbon, and then the sulfur dioxide and the nitrogen dioxide are introduced with oxygen and concentrated to form closed-loop substance circulation; therefore, the invention forms a closed loop aiming at the recovery of Au in the waste Au/C catalyst with high carbon content, effectively reduces the consumption of aqua regia and nitric acid, and saves the recovery cost.|DRAWINGS DESCRIPTION|[0059] Fig. 1 is a flow chart of a method for recovering gold in a carbon gold catalyst according to the invention.|INVENTION MODE|Detailed Description|[0060] In order to further explain the technical solution of the present invention, the present invention is explained in detail by the following specific examples.|[0061] Example 1|[0062] The embodiment discloses a method for recovering gold from a carbon gold catalyst, wherein the process flow is shown in fig. 1, and the method comprises the following steps:|[0063] s1, ball-milling and crushing the waste Au/C catalyst, wherein the particle size of the crushed Au/C catalyst is 15 microns;|[0064] s2, removing carbon by concentrated sulfuric acid for the first time;|[0065] the method comprises the following steps of (1) heating concentrated sulfuric acid to the concentration of 9.2mo1/L to 100 ℃, adding waste Au/C catalyst powder into the concentrated sulfuric acid, wherein the ratio of the powder mass to the concentrated sulfuric acid volume is 20g;|[0066] the concentrated sulfuric acid obtained by S2 recovery can be introduced into S2 again for use;|[0067] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0068] washing 3 times with the concentration of the concentrated nitric acid of 14mol/L, recovering the generated nitrogen dioxide to obtain nitric acid, and introducing S3 for recycling after concentration;|[0069] s4, soaking the solid obtained in the step S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, wherein the mass volume of the solid obtained in the step S3 and the aqua regia is 1g and 1ml, and reacting for 20min; reaction of Au with aqua regia to produce H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0070] s5, heating and evaporating the solution obtained in the S4, and evaporating to remove the residual HNO 3 And HCl to obtain gold trichloride;|[0071] s6, adjusting the pH value to 5 by hydrochloric acid in gold trichloride, adding a reducing agent hydrazine, wherein the stoichiometric ratio of hydrazine to gold is 3:4, fully stirring and reducing to obtain spongy crude gold;|[0072] s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks;|[0073] washing the sponge rough gold with nitric acid, filtering, cleaning, drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass of borax and the sponge rough gold is 1.|[0074] Example 2|[0075] The embodiment discloses a method for recovering gold from a carbon gold catalyst, wherein the process flow is shown in fig. 1, and the method comprises the following steps:|[0076] s1, ball-milling and crushing the waste Au/C catalyst, wherein the particle size of the crushed Au/C catalyst is 12 microns;|[0077] s2, removing carbon by concentrated sulfuric acid for the first time;|[0078] the concentrated sulfuric acid concentration is 11mo1/L, the concentrated sulfuric acid is heated to 90 ℃, waste Au/C catalyst powder is added into the concentrated sulfuric acid, the ratio of the powder mass to the concentrated sulfuric acid volume is 30g;|[0079] the concentrated sulfuric acid obtained by S2 recovery can be introduced into S2 again for use;|[0080] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0081] washing 3 times with concentrated nitric acid with concentration of 15mol/L, recovering the generated nitrogen dioxide to obtain nitric acid, and introducing S3 for recycling after concentration;|[0082] s4, soaking the solid obtained in the step S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, wherein the mass volume of the solid obtained in the step S3 and the aqua regia is 1g; reaction of Au with aqua regia to produce H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0083] s5, heating and evaporating the solution obtained in the S4, and evaporating to remove residual HNO 3 And HCl to obtain gold trichloride;|[0084] s6, adjusting the pH value to 5 by hydrochloric acid in gold trichloride, adding a reducing agent hydrazine, wherein the stoichiometric ratio of hydrazine to gold is 3:4, fully stirring and reducing to obtain spongy crude gold;|[0085] s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks;|[0086] washing the sponge rough gold with nitric acid, filtering, cleaning, drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass of borax and the sponge rough gold is 1.|[0087] Example 3|[0088] The embodiment discloses a method for recovering gold from a carbon gold catalyst, wherein the process flow is shown in fig. 1, and the method comprises the following steps:|[0089] s1, ball-milling and crushing the waste Au/C catalyst, wherein the particle size of the crushed Au/C catalyst is 9 microns;|[0090] s2, removing carbon by concentrated sulfuric acid for the first time;|[0091] the concentrated sulfuric acid concentration is 13mo1/L, the concentrated sulfuric acid is heated to 100 ℃, waste Au/C catalyst powder is added into the concentrated sulfuric acid, the ratio of the powder mass to the concentrated sulfuric acid volume is 40g (1L), the mixture is stirred and reacts for 30min, the generated sulfur dioxide is recycled, the sulfuric acid is concentrated into the concentrated sulfuric acid, and the concentrated sulfuric acid is filtered to obtain a gold-containing solid;|[0092] the concentrated sulfuric acid obtained by S2 recovery can be introduced into S2 again for use;|[0093] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0094] washing for 2 times with the concentration of the concentrated nitric acid being 16mol/L, recovering the generated nitrogen dioxide to obtain nitric acid, and introducing S3 for recycling after concentration;|[0095] s4, the solid from the S3 is in the kingSoaking and dissolving Au and the residual carbon surrounded by Au in water, wherein the mass volume of the solid obtained by S3 and the aqua regia is 1g; reaction of Au with aqua regia to produce H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0096] s5, heating and evaporating the solution obtained in the S4, and evaporating to remove residual HNO 3 And HCl to obtain gold trichloride;|[0097] s6, adjusting the pH value to 5 by hydrochloric acid in gold trichloride, adding a reducing agent hydrazine, wherein the stoichiometric ratio of hydrazine to gold is 3:4, fully stirring and reducing to obtain spongy crude gold;|[0098] s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks;|[0099] washing the sponge rough gold with nitric acid, filtering, cleaning, drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass of borax and the sponge rough gold is 1.|[0100] Example 4|[0101] The embodiment discloses a method for recovering gold from a carbon gold catalyst, wherein the process flow is shown in fig. 1, and the method comprises the following steps:|[0102] s1, ball-milling and crushing the waste Au/C catalyst, wherein the particle size of the crushed Au/C catalyst is 5 micrometers;|[0103] s2, removing carbon by concentrated sulfuric acid at one time;|[0104] the concentrated sulfuric acid concentration is 16mo1/L, the concentrated sulfuric acid is heated to 100 ℃, waste Au/C catalyst powder is added into the concentrated sulfuric acid, the ratio of the powder mass to the concentrated sulfuric acid volume is 40g;|[0105] the concentrated sulfuric acid obtained by S2 recovery can be introduced into S2 again for use;|[0106] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0107] washing for 2 times with the concentration of 17mol/L concentrated nitric acid, recovering the generated nitrogen dioxide to obtain nitric acid, and introducing S3 for recycling after concentration;|[0108] and S4, soaking the solid obtained through the S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, wherein the mass volume of the solid obtained through the S3 and the aqua regia is 1g.1ml, and reacting for 30min; reaction of Au with aqua regia to produce H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0109] s5, heating and evaporating the solution obtained in the S4, and evaporating to remove residual HNO 3 And HCl to obtain gold trichloride;|[0110] s6, adjusting the pH value to 5 by hydrochloric acid in gold trichloride, adding a reducing agent hydrazine, wherein the stoichiometric ratio of hydrazine to gold is 3:4, fully stirring and reducing to obtain spongy crude gold;|[0111] s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks;|[0112] washing the sponge rough gold with nitric acid, filtering, cleaning, drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass of borax and the sponge rough gold is 1.|[0113] Comparative example|[0114] The comparative example discloses a method for recovering gold in a carbon gold catalyst, which specifically comprises the following steps:|[0115] firstly, calcining the gold-carbon catalyst to be recovered at a high temperature of 800 ℃ for 5 hours;|[0116] and step two, dissolving the calcined powder by using aqua regia, and solidifying: nitric acid =1g:1mL;|[0117] thirdly, evaporating the solution to obtain gold trichloride;|[0118] fourthly, adding hydrochloric acid into the product obtained in the third step, and adjusting the pH value to 5;|[0119] fifthly, according to the stoichiometric ratio of hydrazine to gold of 3:4, adding hydrazine, and fully stirring to obtain sponge crude gold;|[0120] sixthly, washing the sponge rough gold with nitric acid, filtering, cleaning and drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass ratio of the borax to the sponge rough gold is 1:10; smelting the mixture into pure gold blocks at 1100 ℃ to obtain pure gold.|[0121] Test examples 1 to 4 and comparative example the recovery rates for gold are shown in table 1, specific test methods, recovery = mass of recovered gold/content of gold in catalyst 100%;|[0122] the catalyst to be recovered used in the test was a simulated deactivated catalyst: the catalyst with known gold content is mixed with organic substances such as lactic acid, aldehydes and the like to be recovered into the recovered catalyst for artificial recovery.|[0123] Table 1 examples 1 to 4 and comparative example gold recovery tables|[0124] Group ofRecovery (%)Comparative example 192.1Example 198.3Example 298.4Example 399.1Example 499.2|[0125] The recovery process provided by the invention has higher recovery rate than the recovery of the comparative solid, and the main reason is that the sulfuric acid and the nitric acid are distributed for two-step decarbonization, the carbon is fully oxidized, the gold loss is avoided, meanwhile, after the powder is put into a reaction tank, the gold is not dissolved under the control of reaction conditions, and the gold is fully ensured to be completely dissolved in the aqua regia; the nitric acid is used for washing, carbon which is not removed in the solid reactant can be discharged in advance, and the nitric acid in the king water is ensured to be completely used for dissolving gold; thereby improving the recovery rate.|[0126] The production process provided by the invention effectively shortens the production time, the specific production time is the actual production time, the actual production time comprises the steps, the transfer among the steps, the manual shift to the shift change, and the calculated actual production time, and the specific data is shown in the table 2.|[0127] Table 2 comparison of time-consuming production for examples 1 to 4 and comparative example recovery|[0128] |[0129] |[0130] The recovery scheme provided by the invention does not need high-temperature calcination, heating preheating and cooling processes, so that the time consumption is short, and in the technical route provided by the invention, liquid reaction can be continuously carried out in a reaction tank, the time for changing materials in batch production is saved, and the industrial requirements are met.|[0131] The recycling profits of examples 1 to 4 and comparative example were further calculated by the following specific calculation formula:|[0132] the recovery profit = (mass of gold recovered per ton of spent catalyst:price) - (cost of per ton of spent catalyst purchase + electricity charge + labor charge + reagent charge + equipment loss), and the recovery profit is shown in table 3.|[0133] Table 3 examples 1 to 4 and comparative examples recovery profits|[0134] Group ofProfit (ten thousand yuan/ton)Comparative example 112Example 138Example 241Example 343Example 443|[0135] The recovery process provided by the invention is short in time consumption and low in energy consumption, and simultaneously, sulfuric acid with lower price is selected for carbon removal, and all acids can be recycled, so that the profit of the invention is far greater than that of a comparative example. (CN115852159)|TECHNICAL FIELD|[0001] The invention relates to a precious metal recovery technology, in particular to a mild method for recovering gold from carbon gold.|BACKGROUND ART|[0002] The carbon-supported gold is widely applied to the production of chemical products, such as the catalytic combustion of hydrocarbons, water gas conversion, liquid-phase chemical oxidation reaction and the like, and effectively improves the reaction rate and degree. The invention patents of CN105107498B and CN112156809A both describe the preparation method of carbon-supported gold catalyst, but as the catalyst, the reaction temperature is too high along with the prolonging of the service time, and agglomeration is generated; or the surface cannot be removed in time because of excessive covering of reactants or products; the catalytic efficiency will gradually decrease to a point of failure and be discarded. However, gold, as a noble metal, is expensive, resulting in a high cost of gold-carbon catalyst, which should be efficiently recovered.|[0003] The common method in the existing technical scheme aiming at gold recovery is to calcine at high temperature to remove carbon, the high-temperature carbon removal process has large energy consumption and causes high recovery cost, and in the calcination process, part of carbon carriers are not removed completely because the temperature is less than 1000 ℃; the residual carbon is contacted with oxidizing acid capable of dissolving gold in the soaking process, and the carbon carrier reacts with the oxidizing acid to dilute the concentration of the oxidizing acid, so that the dissolution of gold is influenced, and the recovery of precious metals is not facilitated.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a method for recovering gold in a carbon gold catalyst, which can be used for recycling substances participating in recovery to form a closed loop while recovering gold mildly, so that the effective acid concentration of gold dissolution is ensured, and the recovery of precious metals is promoted.|[0005] In order to solve the technical problem, the technical scheme of the invention is as follows: a method for recovering gold in a carbon gold catalyst comprises the following steps:|[0006] s1, crushing the waste Au/C catalyst, wherein the particle size is 5-15 mu m after crushing;|[0007] s2, soaking the Au/C catalyst in concentrated sulfuric acid for primary decarbonization;|[0008] the process conditions for the primary carbon removal are as follows:|[0009] heating concentrated sulfuric acid to 80-100 ℃;|[0010] adding Au/C powder into the heated concentrated sulfuric acid;|[0011] stirring and reacting for 20-40 min;|[0012] recovering the generated sulfur dioxide;|[0013] filtering the solid;|[0014] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0015] s4, soaking the solid of the S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, and reacting Au with the aqua regia to generate H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0016] s5, heating and evaporating the solution obtained in the S4, and evaporating the residual HNO 3 And HCl to obtain gold trichloride;|[0017] s6, adding a reducing agent into the gold trichloride, and reducing to obtain spongy crude gold;|[0018] and S7, purifying the crude gold obtained in the S6 to obtain pure gold blocks.|[0019] The preferred process conditions for sulfur dioxide recovery in S2 are as follows:|[0020] introducing water to form sulfurous acid, and introducing oxygen into the sulfurous acid to obtain sulfuric acid;|[0021] the reaction principle is as follows:|[0022] 2H 2 SO 3 +O 2 →2H 2 SO 4|[0023] heating and concentrating sulfuric acid to obtain concentrated sulfuric acid, and introducing the concentrated sulfuric acid into S2 for recycling.|[0024] The preferred process conditions for the recovery of nitric oxide and nitrogen dioxide produced by S3 and S4 are as follows:|[0025] introducing water and oxygen into the residual nitrogen-containing gas for many times to convert the nitrogen-containing gas into nitric acid;|[0026] the reaction principle is as follows:|[0027] 3NO 2 +H 2 O→2HNO 3 +NO;|[0028] 2NO+O 2 →2NO 2 ;|[0029] heating and concentrating nitric acid to obtain concentrated nitric acid, and adding the concentrated nitric acid into S3 for recycling.|[0030] The preferable specific manner of reduction of gold trichloride in S6 is as follows: dissolving gold trichloride and hydrazine in hydrochloric acid, and forming HAuCl by chloroauric acid and hydrochloric acid 4 Hydrazine with hydrochloric acid to form N 2 H 5 Cl, reduction reaction as follows:|[0031] 3N 2 H 5 Cl+4HAuCl 4 →3N 2 +4Au +19HCl. The invention reduces the gold in the chloroauric acid to the simple substance gold particles for dissolving out, and obtains the crude gold filled with sponge.|[0032] Preferably, the purification process conditions in S7 include the following steps:|[0033] s71, washing the sponge coarse gold with nitric acid, filtering, cleaning and drying;|[0034] s72, putting the gold mud into a magnetic crucible, adding 10-15 wt% of borax, and smelting into pure gold blocks at 1000-1100 ℃.|[0035] Preferably, the concentrated sulfuric acid concentration for the first carbon removal in S2 is 9.2mo1/L to 16mol/L.|[0036] The mass volume ratio of the Au/C powder to the concentrated sulfuric acid is preferably (20 g to 40 g): 1L of the total amount of the active ingredients. The invention adopts the showering nitric acid, on one hand, the concentration of the concentrated nitric acid is ensured to be high enough; the method avoids the problems that the effective collision of nitrate radicals and carbon-containing substances is less due to insufficient concentration of nitric acid, and the thorough removal of the carbon-containing substances cannot be ensured; on the other hand, concentrated nitric acid is unstable and has chemical reaction when meeting light, the concentration is too high, the concentrated nitric acid is easy to volatilize and decompose, the production condition is too harsh, and light shielding or matching is needed, so that the concentrated nitric acid effectively ensures the flow of the concentrated nitric acid relative to solid matters to promote the decomposition of carbon in the solid matters by spraying, and the solid matters are fully covered by the fluidity of liquid to form effective contact of the solid phases and the liquid phases.|[0037] Preferably, the concentration of the concentrated nitric acid for spraying and washing the solid in the S2 in the S3 is 14mol/L to 17mol/L. Concentrated sulfuric acid which is used for primary carbon removal and can not further dissolve carbon is remained in the solid, and is not beneficial to hydrazine participation in reduction, so that when nitric acid is used for washing, sulfuric acid with lower concentration has weak reaction capacity with carbon, N has stronger electronegativity than S, concentrated nitric acid is easier to react with carbon, when nitric acid is sprayed and washed, nitrate radicals react with carbon-containing substances in preference to remove carbon for the second time, sulfate radicals in the system flow away along with unreacted nitric acid, and residual sulfuric acid is effectively removed.|[0038] Preferably, the mass of the Au/C catalyst to be recovered accounts for 100 parts, wherein Au accounts for 10-30 parts, and the balance is carbon.|[0039] The preferred preparation method of the Au/C catalyst comprises the following steps:|[0040] s11, mixing HAuCl 4 Mixing the solution and the active carbon dispersed by using alkali liquor according to the mass part ratio, and uniformly stirring;|[0041] wherein the adjusting substance of the alkali liquor is NaHCO 3 ;|[0042] S12, continuously stirring; standing; and filtering, reducing and drying to obtain the Au/C catalyst.|[0043] By adopting the technical scheme, the invention has the beneficial effects that:|[0044] the main reason for the inactivation of the Au/C catalyst is that the surface of the catalyst is coated by carbon-containing organic matters such as aldehydes and acids, so that the catalyst cannot generate a catalytic action, and the carbon-containing organic matters also exist in the catalyst to be recovered; the caking of the catalyst can be caused in the using process, and the catalytic performance is further reduced; the invention crushes the carbon with organic matter as load and the gold particles with catalytic activity, firstly, the concentrated sulfuric acid is used for soaking under heating condition, the concentrated sulfuric acid has strong dehydration and oxidation effects, can convert the carbon-containing organic matter into carbon dioxide and water, and can also generate the carbon dioxide and the water by dissolving the carrier carbon material with the concentrated sulfuric acid; because the mass ratio of organic carbon to inorganic carbon in the waste catalyst particles is high, the organic carbon and the inorganic carbon are removed by soaking in concentrated sulfuric acid, and the waste catalyst particles are further crushed by using a chemical reaction consumption mode; the specific reaction mode is as follows:|[0045] C+2H 2 SO 4 (concentrated) → CO 2 ↑+2SO 2 ↑+2H 2 O;|[0046] The concentrated sulfuric acid selectively consumes carbon materials in the catalyst compound under the heating condition, the crushed particle structure of the Au/C catalyst is decomposed and broken in the process, and a certain amount of sulfuric acid which is not enough to dissolve organic carbon and inorganic carbon is adsorbed in the activated carbon due to the adsorbability of the activated carbon;|[0047] after the waste catalyst is subjected to primary decarbonization, the rest part of the active carbon further limits the decarbonization due to the adsorption of sulfonic acid groups and the reduction of the concentration of concentrated sulfuric acid;|[0048] then, concentrated nitric acid is used for washing Au/C catalyst particles which are subjected to preliminary carbon removal and crushing by concentrated sulfuric acid, and after organic carbon on the surfaces of the catalyst particles is removed, the active carbon connected with Au is further subjected to oxidation reduction by utilizing stronger oxidizability of the concentrated nitric acid to remove the active carbon; a large amount of concentrated sulfuric acid and concentrated nitric acid are used for consuming carbon in the waste catalyst, and aqua regia for dissolving Au is guaranteed to have stable concentration, so that Au and residual carbon are quickly dissolved;|[0049] the concentrated sulfuric acid is removed in the concentrated nitric acid spraying process, simultaneously, carbon materials in Au/C catalyst particles are thoroughly and selectively removed, and the Au/C catalyst particles with smaller sizes are obtained, and the specific reaction principle is as follows:|[0050] C+4HNO 3 (concentrated) → CO 2 ↑+4NO 2 ↑+2H 2 O;|[0051] The concentrated sulfuric acid which is used for removing carbon twice and can remove the concentrated sulfuric acid which is remained after the carbon is removed once, and the sulfuric acid reacts with hydrazine to obtain N 2 H 4 +H 2 SO 4 →N 2 H 6 SO 4 Not beneficial to the effective reduction of Au;|[0052] the Au particles which are crushed by concentrated sulfuric acid and concentrated nitric acid and are decarbonized and still contain a certain amount of residual carbon are immersed in aqua regia to obtain chloroauric acid, and the reaction mechanism of Au and aqua regia is as follows:|[0053] Au+HNO 3 +4HCl→H[AuCl 4 ]+NO↑+2H 2 O;|[0054] heating and decomposing chloroauric acid to obtain AuCl 3 The specific principle is as follows:|[0055] H[AuCl 4 ]→HCl+AuCl 3 ;|[0056] then reducing and purifying to obtain pure gold;|[0057] aiming at the existence of a large amount of organic carbon and inorganic carbon in the waste Au/C catalyst, concentrated sulfuric acid is firstly used for removing carbon for the first time; then, carrying out secondary decarbonization by using concentrated nitric acid with higher oxidability; after most of carbon is removed, the aqua regia is used for effectively dissolving gold, so that the problems that the concentration of nitric acid and hydrochloric acid in the aqua regia is reduced due to the consumption of carbon materials, the dissolution of Au is slowed and incomplete, and the gold recovery is not facilitated due to the preferential reaction of the aqua regia with carbon materials caused by the existence of carbon when the gold is dissolved due to the existence of a large amount of organic carbon and inorganic carbon are avoided;|[0058] in the prior art, carbon is removed by calcination, and the acid substances are recycled by oxidation-reduction reaction in the process of removing the carbon; the invention utilizes the addition sequence of concentrated sulfuric acid, concentrated nitric acid and aqua regia to recover sulfur dioxide and nitrogen dioxide corresponding to the used concentrated sulfuric acid and concentrated nitric acid by oxidation reduction of organic carbon and inorganic carbon, and then the sulfur dioxide and the nitrogen dioxide are introduced with oxygen and concentrated to form closed-loop substance circulation; therefore, the invention forms a closed loop aiming at the recovery of Au in the waste Au/C catalyst with high carbon content, effectively reduces the consumption of aqua regia and nitric acid, and saves the recovery cost.|DRAWINGS DESCRIPTION|[0059] Fig. 1 is a flow chart of a method for recovering gold in a carbon gold catalyst according to the invention.|INVENTION MODE|Detailed Description|[0060] In order to further explain the technical solution of the present invention, the present invention is explained in detail by the following specific examples.|[0061] Example 1|[0062] The embodiment discloses a method for recovering gold from a carbon gold catalyst, wherein the process flow is shown in fig. 1, and the method comprises the following steps:|[0063] s1, ball-milling and crushing the waste Au/C catalyst, wherein the particle size of the crushed Au/C catalyst is 15 microns;|[0064] s2, removing carbon by concentrated sulfuric acid for the first time;|[0065] the method comprises the following steps of (1) heating concentrated sulfuric acid to the concentration of 9.2mo1/L to 100 ℃, adding waste Au/C catalyst powder into the concentrated sulfuric acid, wherein the ratio of the powder mass to the concentrated sulfuric acid volume is 20g;|[0066] the concentrated sulfuric acid obtained by S2 recovery can be introduced into S2 again for use;|[0067] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0068] washing 3 times with the concentration of the concentrated nitric acid of 14mol/L, recovering the generated nitrogen dioxide to obtain nitric acid, and introducing S3 for recycling after concentration;|[0069] s4, soaking the solid obtained in the step S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, wherein the mass volume of the solid obtained in the step S3 and the aqua regia is 1g and 1ml, and reacting for 20min; reaction of Au with aqua regia to produce H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0070] s5, heating and evaporating the solution obtained in the S4, and evaporating to remove the residual HNO 3 And HCl to obtain gold trichloride;|[0071] s6, adjusting the pH value to 5 by hydrochloric acid in gold trichloride, adding a reducing agent hydrazine, wherein the stoichiometric ratio of hydrazine to gold is 3:4, fully stirring and reducing to obtain spongy crude gold;|[0072] s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks;|[0073] washing the sponge rough gold with nitric acid, filtering, cleaning, drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass of borax and the sponge rough gold is 1.|[0074] Example 2|[0075] The embodiment discloses a method for recovering gold from a carbon gold catalyst, wherein the process flow is shown in fig. 1, and the method comprises the following steps:|[0076] s1, ball-milling and crushing the waste Au/C catalyst, wherein the particle size of the crushed Au/C catalyst is 12 microns;|[0077] s2, removing carbon by concentrated sulfuric acid for the first time;|[0078] the concentrated sulfuric acid concentration is 11mo1/L, the concentrated sulfuric acid is heated to 90 ℃, waste Au/C catalyst powder is added into the concentrated sulfuric acid, the ratio of the powder mass to the concentrated sulfuric acid volume is 30g;|[0079] the concentrated sulfuric acid obtained by S2 recovery can be introduced into S2 again for use;|[0080] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0081] washing 3 times with concentrated nitric acid with concentration of 15mol/L, recovering the generated nitrogen dioxide to obtain nitric acid, and introducing S3 for recycling after concentration;|[0082] s4, soaking the solid obtained in the step S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, wherein the mass volume of the solid obtained in the step S3 and the aqua regia is 1g; reaction of Au with aqua regia to produce H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0083] s5, heating and evaporating the solution obtained in the S4, and evaporating to remove residual HNO 3 And HCl to obtain gold trichloride;|[0084] s6, adjusting the pH value to 5 by hydrochloric acid in gold trichloride, adding a reducing agent hydrazine, wherein the stoichiometric ratio of hydrazine to gold is 3:4, fully stirring and reducing to obtain spongy crude gold;|[0085] s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks;|[0086] washing the sponge rough gold with nitric acid, filtering, cleaning, drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass of borax and the sponge rough gold is 1.|[0087] Example 3|[0088] The embodiment discloses a method for recovering gold from a carbon gold catalyst, wherein the process flow is shown in fig. 1, and the method comprises the following steps:|[0089] s1, ball-milling and crushing the waste Au/C catalyst, wherein the particle size of the crushed Au/C catalyst is 9 microns;|[0090] s2, removing carbon by concentrated sulfuric acid for the first time;|[0091] the concentrated sulfuric acid concentration is 13mo1/L, the concentrated sulfuric acid is heated to 100 ℃, waste Au/C catalyst powder is added into the concentrated sulfuric acid, the ratio of the powder mass to the concentrated sulfuric acid volume is 40g (1L), the mixture is stirred and reacts for 30min, the generated sulfur dioxide is recycled, the sulfuric acid is concentrated into the concentrated sulfuric acid, and the concentrated sulfuric acid is filtered to obtain a gold-containing solid;|[0092] the concentrated sulfuric acid obtained by S2 recovery can be introduced into S2 again for use;|[0093] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0094] washing for 2 times with the concentration of the concentrated nitric acid being 16mol/L, recovering the generated nitrogen dioxide to obtain nitric acid, and introducing S3 for recycling after concentration;|[0095] s4, the solid from the S3 is in the kingSoaking and dissolving Au and the residual carbon surrounded by Au in water, wherein the mass volume of the solid obtained by S3 and the aqua regia is 1g; reaction of Au with aqua regia to produce H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0096] s5, heating and evaporating the solution obtained in the S4, and evaporating to remove residual HNO 3 And HCl to obtain gold trichloride;|[0097] s6, adjusting the pH value to 5 by hydrochloric acid in gold trichloride, adding a reducing agent hydrazine, wherein the stoichiometric ratio of hydrazine to gold is 3:4, fully stirring and reducing to obtain spongy crude gold;|[0098] s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks;|[0099] washing the sponge rough gold with nitric acid, filtering, cleaning, drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass of borax and the sponge rough gold is 1.|[0100] Example 4|[0101] The embodiment discloses a method for recovering gold from a carbon gold catalyst, wherein the process flow is shown in fig. 1, and the method comprises the following steps:|[0102] s1, ball-milling and crushing the waste Au/C catalyst, wherein the particle size of the crushed Au/C catalyst is 5 micrometers;|[0103] s2, removing carbon by concentrated sulfuric acid at one time;|[0104] the concentrated sulfuric acid concentration is 16mo1/L, the concentrated sulfuric acid is heated to 100 ℃, waste Au/C catalyst powder is added into the concentrated sulfuric acid, the ratio of the powder mass to the concentrated sulfuric acid volume is 40g;|[0105] the concentrated sulfuric acid obtained by S2 recovery can be introduced into S2 again for use;|[0106] s3, washing the Au/C catalyst subjected to primary decarbonization by concentrated nitric acid, and removing concentrated sulfuric acid on the surface of the solid while performing secondary decarbonization;|[0107] washing for 2 times with the concentration of 17mol/L concentrated nitric acid, recovering the generated nitrogen dioxide to obtain nitric acid, and introducing S3 for recycling after concentration;|[0108] and S4, soaking the solid obtained through the S3 in aqua regia to dissolve Au and residual carbon surrounded by Au, wherein the mass volume of the solid obtained through the S3 and the aqua regia is 1g.1ml, and reacting for 30min; reaction of Au with aqua regia to produce H [ AuCl ] 4 ]The carbon reaction is the recovery of nitrogen dioxide and carbon dioxide;|[0109] s5, heating and evaporating the solution obtained in the S4, and evaporating to remove residual HNO 3 And HCl to obtain gold trichloride;|[0110] s6, adjusting the pH value to 5 by hydrochloric acid in gold trichloride, adding a reducing agent hydrazine, wherein the stoichiometric ratio of hydrazine to gold is 3:4, fully stirring and reducing to obtain spongy crude gold;|[0111] s7, purifying the crude gold obtained in the S6 to obtain pure gold blocks;|[0112] washing the sponge rough gold with nitric acid, filtering, cleaning, drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass of borax and the sponge rough gold is 1.|[0113] Comparative example|[0114] The comparative example discloses a method for recovering gold in a carbon gold catalyst, which specifically comprises the following steps:|[0115] firstly, calcining the gold-carbon catalyst to be recovered at a high temperature of 800 ℃ for 5 hours;|[0116] and step two, dissolving the calcined powder by using aqua regia, and solidifying: nitric acid =1g:1mL;|[0117] thirdly, evaporating the solution to obtain gold trichloride;|[0118] fourthly, adding hydrochloric acid into the product obtained in the third step, and adjusting the pH value to 5;|[0119] fifthly, according to the stoichiometric ratio of hydrazine to gold of 3:4, adding hydrazine, and fully stirring to obtain sponge crude gold;|[0120] sixthly, washing the sponge rough gold with nitric acid, filtering, cleaning and drying, putting gold mud into a magnetic crucible, adding borax, wherein the mass ratio of the borax to the sponge rough gold is 1:10; smelting the mixture into pure gold blocks at 1100 ℃ to obtain pure gold.|[0121] Test examples 1 to 4 and comparative example the recovery rates for gold are shown in table 1, specific test methods, recovery = mass of recovered gold/content of gold in catalyst 100%;|[0122] the catalyst to be recovered used in the test was a simulated deactivated catalyst: the catalyst with known gold content is mixed with organic substances such as lactic acid, aldehydes and the like to be recovered into the recovered catalyst for artificial recovery.|[0123] Table 1 examples 1 to 4 and comparative example gold recovery tables|[0124] Group ofRecovery (%)Comparative example 192.1Example 198.3Example 298.4Example 399.1Example 499.2|[0125] The recovery process provided by the invention has higher recovery rate than the recovery of the comparative solid, and the main reason is that the sulfuric acid and the nitric acid are distributed for two-step decarbonization, the carbon is fully oxidized, the gold loss is avoided, meanwhile, after the powder is put into a reaction tank, the gold is not dissolved under the control of reaction conditions, and the gold is fully ensured to be completely dissolved in the aqua regia; the nitric acid is used for washing, carbon which is not removed in the solid reactant can be discharged in advance, and the nitric acid in the king water is ensured to be completely used for dissolving gold; thereby improving the recovery rate.|[0126] The production process provided by the invention effectively shortens the production time, the specific production time is the actual production time, the actual production time comprises the steps, the transfer among the steps, the manual shift to the shift change, and the calculated actual production time, and the specific data is shown in the table 2.|[0127] Table 2 comparison of time-consuming production for examples 1 to 4 and comparative example recovery|[0128] |[0129] |[0130] The recovery scheme provided by the invention does not need high-temperature calcination, heating preheating and cooling processes, so that the time consumption is short, and in the technical route provided by the invention, liquid reaction can be continuously carried out in a reaction tank, the time for changing materials in batch production is saved, and the industrial requirements are met.|[0131] The recycling profits of examples 1 to 4 and comparative example were further calculated by the following specific calculation formula:|[0132] the recovery profit = (mass of gold recovered per ton of spent catalyst:price) - (cost of per ton of spent catalyst purchase + electricity charge + labor charge + reagent charge + equipment loss), and the recovery profit is shown in table 3.|[0133] Table 3 examples 1 to 4 and comparative examples recovery profits|[0134] Group ofProfit (ten thousand yuan/ton)Comparative example 112Example 138Example 241Example 343Example 443|[0135] The recovery process provided by the invention is short in time consumption and low in energy consumption, and simultaneously, sulfuric acid with lower price is selected for carbon removal, and all acids can be recycled, so that the profit of the invention is far greater than that of a comparative example. Family Number|(104319154)|104319154|Abstract|(CN115852159 A)|The invention discloses a method for recovering gold in a carbon - gold catalyst . The method comprises the following steps : S1 , crushing a waste Au / C catalyst ; s2 , soaking the Au / C catalyst in concentrated sulfuric acid for primary carbon removal ; s3 , washing the Au / C catalyst subjected to primary carbon removal with concentrated nitric acid , and removing concentrated sulfuric acid on the surface of a solid while secondary carbon removal ; s4 , the solid obtained in S3 is soaked in aqua regia to dissolve Au and residual carbon surrounded by Au , Au and aqua regia react to generate H [ AuCl4 ] , and the carbon reaction is gas recovery ; s5 , heating and evaporating the solution obtained in the step S4 , and evaporating residual HNO3 and HCl to obtain gold trichloride ; s6 , a reducing agent is added into the gold trichloride , and spongy crude gold is obtained through reduction ; s7 , purifying the crude gold obtained in the step S6 to obtain a pure gold block ; while the gold is mildly recovered , the substance participating in the recovery can be recycled to form a closed loop , so that the effective acid concentration for dissolving the gold is guaranteed , and the recovery of the noble metal is promoted . |IPC codes|(CN115852159 A)|B01J - 023/50 |B01J - 023/96 | Chemical engineering|Materials, metallurgy B01J-023/50|B01J-023/96|C22B-007/00|C22B-011/00 B01J-023/50|B01J-023/96|C22B-007/00|C22B-011/00 CN116622996 CN116622996 106220685 WHO=Examiner SELF=N CAT=A CN106498178|CN114058864|CN206564083U|JP2017133084 CN106498178 75646784 WHO=Examiner SELF=N CAT=X|CN114058864 98762695 WHO=Examiner SELF=N CAT=A|CN206564083U 77504844 WHO=Examiner SELF=N CAT=A|JP2017133084 76910189 WHO=Examiner SELF=N CAT=A 刘增利主编;闫彬,张万程,刘雄兵,李云华,赵率,刘光寨编: &quot;《倍速学习法 高中化学 必修1 RJ版 2016版》&quot;, 30 April 2013, 北京:开明出版社, pages: 138 - 150 (Cat. A) CN106498178; JP2017133084; CN206564083U; CN114058864 REVOKED (CN115852159)|REVOKED DEAD (CN115852159)|DEAD (CN115852159)|LEGAL DETAILS FOR CN115852159|Actual or expected expiration date=2025-12-02|Legal state=DEAD|Status=REVOKED|Event publication date=2022-12-23|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211664591|Application date=2022-12-23|Standardized application number=2022CN-1664591|Event publication date=2023-03-28|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115852159|Publication stage code=A|Publication date=2023-03-28|Standardized publication number=CN115852159|Event publication date=2023-03-28|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-04-14|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-12-02|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQAvH+1L7Xd6Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067116757&ekey=2140&xpn=CN115852159&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=R2euZiT2wY8mCAyWm1F3m5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN115852159)|CN (CN115852159)|NAME=Zhejiang Shengyang Renewable Resources Technology Co.,Ltd. , COUNTRY=CN (CN115852159)|NAME=HU ENHAN;JINHUA WUSHI PATENT AGENCY (GENERAL PARTNERSHIP) , REG=33340 (CN115852159)|NAME=XU YIZHEN|NAME=ZHANG JIANPING|NAME=ZHOU SHUIJUN|NAME=XU SHENGYANG|NAME=YANG ZHANGBAO 0 1 Titre: (CN115852159)|Method for recovering gold in carbon-gold catalyst Résumé: (CN115852159)|The invention discloses a method for recovering gold in a carbon-gold catalyst. The method comprises the following steps: S1, crushing a waste Au/C catalyst; s2, soaking the Au/C catalyst in concentrated sulfuric acid for primary carbon removal; s3, washing the Au/C catalyst subjected to primary carbon removal with concentrated nitric acid, and removing concentrated sulfuric acid on the surface of a solid while secondary carbon removal; s4, the solid obtained in S3 is soaked in aqua regia to dissolve Au and residual carbon surrounded by Au, Au and aqua regia react to generate H [AuCl4], and the carbon reaction is gas recovery; s5, heating and evaporating the solution obtained in the step S4, and evaporating residual HNO3 and HCl to obtain gold trichloride; s6, a reducing agent is added into the gold trichloride, and spongy crude gold is obtained through reduction; s7, purifying the crude gold obtained in the step S6 to obtain a pure gold block; while the gold is mildly recovered, the substance participating in the recovery can be recycled to form a closed loop, so that the effective acid concentration for dissolving the gold is guaranteed, and the recovery of the noble metal is promoted. 70 Abstract gpt-4o-mini no The article focuses on a method for recovering gold from a carbon-gold catalyst, which does not relate to accelerated weathering or CO₂ capture.
71 CN202211188508 CN202211188508 CN115504757|CN115504757 103140257 CN115504757 B 2023-10-03 [CN115504757B]|CN115504757 A 2022-12-23 [CN115504757] 2022-09-27 2022-09-27 2023-10-03|2022-12-23 (CN115504757B)|2023-10-03 (CN115504757)|2042-09-27 (CN115504757)|Method for sealing and carbon fixation of agricultural straw (CN115504757)|The invention discloses an agricultural straw sealing and carbon sequestration method. The method comprises the following steps: step 1, straw collection; step 2, straw crushing operation; step 3, straw compression operation; step 4, drying operation; 5, curing and sealing operation; and 6, carrying out reclamation backfill operation. The method has the advantages that the agricultural straw is directly sealed and stored, the straw is derived from agricultural waste and is low in price and easy to obtain, meanwhile, CO2 trapping action is completed through respiration of the agricultural straw, energy consumption is reduced, carbon emission is reduced, the economic cost is further reduced, the straw is harmless to the environment, the chemical property of a solidified layer is stable, and the method is suitable for industrial production. In addition, the solidified layer is stable in structure, geological accidents are not prone to being caused, and sealed solid straw is greener, safer and risk-free than sealed gaseous or liquid CO2. DONGGUAN UNIVERSITY OF TECHNOLOGY (CN115504757)|DONGGUAN UNIVERSITY OF TECHNOLOGY ([CN])|(CN115504757)|DONGGUAN UNIVERSITY OF TECHNOLOGY ([CN]) HUANG XIA|YU CHUNXUE|ZHENG YUANHUAN|SU MEIRONG|HOU XIAOSHU (CN115504757)|HUANG XIA|YU CHUNXUE|ZHENG YUANHUAN|SU MEIRONG|HOU XIAOSHU|(CN115504757)|HUANG XIA|YU CHUNXUE|ZHENG YUANHUAN|SU MEIRONG|HOU XIAOSHU (CN115504757)|XU YONGLEI;SUZHOU YANSIJIAXIN PATENT AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 32385 (CN115504757)|The existing carbon emission reduction technology is mainly divided into CO 2 The four major links of gathering, transporting, utilizing and sealing and storing are that CO is used as the main body of sealing and storing 2 Or in a gaseous or liquid state, is technically less expensive and has a leakage risk.| (CN115504757)|1. The method for sealing and carbon fixation of the agricultural straw is characterized by comprising the following steps of:step one: collecting straws;step two: crushing straw;step three: compressing straw;step four: drying operation;step five: curing and sealing operation;step six: a reclamation backfilling operation;in the first step, the collected straws are naturally dried, and the moisture content of the straws is 30%;in the second step, a straw pulverizer is adopted to pulverize the collected straws, and the straw pulverizer is started to idle for 2-3 minutes before pulverization, so that the straw pulverizer is carried out after no abnormal phenomenon exists;in the third step, a briquetting machine is adopted to carry out briquetting operation on the crushed straws, the briquetting efficiency is 0.1 ton/hour, and the power is 15 kilowatts;in the fourth step, compressed agricultural straws are dried by hot air, and the moisture content of the straws is reduced to below 2%, so that living environment is not created for microorganisms, and the straws are not decomposed;selecting a proper sealing place, wherein the sealing place is required to have a stable geological structure, a geological layer is dense, bare land, grassland and forest land can be selected for excavation, or a mined pit can be directly utilized for sealing, and then a downstream area with the flow direction of groundwater flow is selected to be far away from a water source, a living area and other protection areas;in the sixth step, a pit for landfill is excavated, the excavation depth is 100-400 m below the ground, the bottom and four walls of the pit are reinforced and impervious by a curing layer, and the excavation area is not more than 100m 2 In order to prevent the ground from sinking, paving a layer of 60 cm-100 cm of the straws pretreated in the first step-the fifth step, paving a layer of quicklime on each layer of straws, compacting and reinforcing, wherein the paving height is not more than 100m below the ground, and the periphery of the layer of straws is covered by a curing layer;the main components of the solidified layer are: 25-55% of mineral powder, 25-55% of silicate cement clinker, 4-10% of adhesion promoter, 2-8% of lime, 2-8% of anhydrite and 1-5% of active magnesium oxide in percentage by mass.| (CN115504757)|The invention discloses a method for sealing and storing agricultural straws to fix carbon, which comprises the following steps: step one: collecting straws; step two: crushing straw; step three: compressing straw; step four: drying operation; step five: curing and sealing operation; step six: and (5) reclamation backfilling operation.|The invention relates to the technical field of carbon emission reduction, in particular to a method for sealing and solidifying carbon by agricultural straws.| (CN115504757)|AGRICULTURAL STRAW(100,32)|SEALING(100,16)|CARBON FIXATION(100,5)|AGRICULTURAL STRAW CARBON FIXATION(100,4)|STRAW PULVERIZER(88,9)|STRAW MOISTURE CONTENT(71,3)|CRUSHING STRAW(68,4)|COMPRESSING STRAW(66,4)|COLLECTING STRAW(64,4)|PULVERIZE COLLECTED STRAW(60,3)|AGRICULTURAL STRAW RESPIRATION(58,3)|AGRICULTURAL STRAW(57,2)|PIT MINING(57,1)|CRUSHED STRAW(45,3)|MOISTURE CONTENT(43,3)|SILICATE CEMENT CLINKER(42,3)|RECLAMATION BACKFILLING OPERATION(41,3)|FOREST SOIL(41,2)|LIVING ENVIRONMENT(40,1)|STRAW(38,15)|STRAW LAYER(38,5)|ABNORMAL PHENOMENON(38,3)|ADHESION PROMOTER(35,3)|COLLECTED STRAW(35,3)|EXCAVATION DEPTH(35,3)|GEOLOGICAL ACCIDENT(34,3)|PAVING HEIGHT(34,2)|SOLIDIFYING CARBON(34,1)|BRIQUETTING MACHINE(33,3)|LAYER SOLIDIFICATION(31,11)|CURING LAYER(29,5)|BRIQUETTING(29,3)|INORGANIC POWDER(27,3)|QUICKLIME LAYER(25,4)|CURING(24,4)|PULVERIZATION(23,3)|ANHYDRITE(21,3)|EXCAVATION(21,3)|GRASSLAND(21,3)|REINFORCING(21,2)|SEALING POSITION(20,6)|COMPACTING(20,3)|MICROORGANISM(19,11)|LANDFILL(19,3)|SILICATE CEMENT(19,3)|EXCAVATION AREA(18,3)|SINKING(17,3)|STABLE GEOLOGICAL STRUCTURE(16,3)|STEP SIX(15,5)|CONTAMINATION(15,3)|LIME(15,3)|TRAPPING(15,3)|DRYING OPERATION(14,4)|SEALING OPERATION(14,4)|ACTIVE MAGNESIUM OXIDE(14,3)|LIVING AREA(14,3)|GEOLOGICAL LAYER(14,2)|SOLID STATE STRAW(14,2)|STEP FOUR(14,2)|AGRICULTURAL WASTE(13,3)|BRIQUETTING OPERATION(13,3)|DOWNSTREAM AREA(13,3)|PROTECTION AREA(13,3)|CARBON EMISSION REDUCTION(11,11)|GROUNDWATER FLOW(11,2)|MAGNESIUM OXIDE(10,3)|DECOMPOSE STRAW(10,2)|CARBON CIRCULATION(8,4)|EARTH RESOURCE(8,2)|COMPRESSED AGRICULTURAL STRAW(8,1)|FUELING CATEGORY(8,1)|SLAKED LIME(7,5)|STEP THREE(7,4)|ECONOMIC COST(7,3)|ISOLATION ROLE(7,2)|EXPLOITED PIT(7,1)|PRETREATED STRAW(7,1)|ENERGY CONSUMPTION(6,4)|CHEMICAL PROPERTY(6,3)|HOT AIR(6,3)|AGRICULTURAL STRAWTHE CARBON EMISSION(6,1)|EXTENSIVE UTILIZATION(6,1)|STRAW BIOMASS(6,1)|SOIL DEPTH(5,2)|AGRICULTURAL STRAW TREATMENT MODE(5,1)|PROCESSING AGRICULTURAL STRAW(5,1)|SEALING YEAR(5,1)|SOIL FERTILITY ENHANCEMENT(5,1)|STRAW PERIPHERY(5,1)|TECHNICAL INNOVATION(5,1)|AWAY(4,3)|BACKFILL(4,2)|FIXING CARBON(4,2)|SOLID STRAW(4,2)|SURVIVAL(4,2)|AMBIENT SOLIDIFIED LAYER(4,1)|ECONOMIC BENEFIT(4,1)|GEOLOGICAL CONDITION(4,1)|LAYING HEIGHT(4,1)|LEAKAGE RISK(4,1)||(CN115504757)|AGRICULTURAL STRAW(100,33)|CARBON SEQUESTRATION(100,9)|SEQUESTRATION(100,6)|FIXING CARBON(100,5)|AGRICULTURAL STRAW CARBON SEQUESTRATION(100,4)|COLLECTING STRAW(46,4)|BRIQUETTING CRUSHED STRAW(39,2)|STRAW PULVERIZER(35,4)|SEQUESTRATION SITE(35,2)|STRAW(32,25)|AGRICULTURAL STRAW RESPIRATORY ACTION(32,2)|STRAW MOISTURE CONTENT(28,5)|RECLAMATION(26,4)|COMPRESSED AGRICULTURAL STRAW(26,3)|GEOLOGICAL ACCIDENT(25,3)|LAYER SOLIDIFICATION(24,15)|COLLECTED STRAW(23,6)|PORTLAND CEMENT CLINKER(22,3)|PERIPHERAL LAND(20,1)|WOODED LAND(19,2)|PARTICULARLYGREEN(19,1)|ABNORMAL PHENOMENON(18,3)|BACKFILLING OPERATION(18,3)|PIT MINING(18,3)|STRAW PERIPHERY(18,3)|LEAKAGE RISK(18,2)|GATHERING ACTION(18,1)|SEALING MAIN(18,1)|CURING(17,4)|STRAW COMPRESSION OPERATION(17,4)|ADHESION PROMOTER(16,3)|GATHERING(16,1)|BRIQUETTING MACHINE(15,3)|PAVING HEIGHT(15,2)|RESPIRATORY SYSTEM ACTION(15,2)|LIVING ENVIRONMENT(14,2)|DECOMPOSITION(14,1)|INORGANIC POWDER(13,3)|QUICKLIME LAYER(13,2)|PULVERIZATION(13,1)|CARBON EMISSION REDUCTION(12,11)|STRAW LAYER(12,3)|PRICE(12,1)|STEP SIX(11,4)|CONTAMINATION(11,3)|SOLID STRAW(11,3)|GROUNDWATER(11,2)|DRYING OPERATION(10,4)|ANHYDRITE(10,3)|DENSE GEOLOGICAL LAYER(10,3)|GRASSLAND(10,3)|COMPACTING(10,2)|LANDFILL(10,2)|STEP FOUR(10,2)|EXTENSIVE UTILIZATION(9,4)|REINFORCING(9,2)|AGRICULTURAL STRAW SELF RESPIRATION(8,1)|DIGGING AREA(7,3)|STABLE GEOLOGICAL STRUCTURE(7,3)|STRAW CRUSHER(7,2)|CARBON CIRCULATION(6,4)|ACTIVE MAGNESIUM OXIDE(6,3)|DOWNSTREAM AREA(6,3)|PROTECTION AREA(6,3)|EARTH RESOURCE(6,2)|HUMAN LIVING AREA(6,1)|SLAKED LIME(5,5)|STEP THREE(5,4)|ECONOMIC COST(5,3)|AGRICULTURAL WASTESIS(5,1)|CRUSHED STRAW(5,1)|LAYING QUICKLIME(5,1)|ENERGY CONSUMPTION(4,4)|CHEMICAL PROPERTY(4,3)|MASS FRACTION(4,3)|LIQUID STATE(4,2)|SOIL DEPTH(4,2)|TRAPPING ACTION(4,2)|FUEL CATEGORY(4,1)|STRAW BIOMASS(4,1)|AGRICULTURAL STRAW TREATMENT MODE(3,1)|CURING STABILITY(3,1)|ECONOMIC BENEFIT(3,1)|GAS STATE(3,1)|PROCESSING AGRICULTURAL STRAW(3,1)|SOIL FERTILITY ENHANCEMENT(3,1)|TECHNICAL INNOVATION(3,1)| (CN115504757)|1. The method for sealing and carbon fixation of the agricultural straw is characterized by comprising the following steps of:|step one: collecting straws;|step two: crushing straw;|step three: compressing straw;|step four: drying operation;|step five: curing and sealing operation;|step six: a reclamation backfilling operation;|in the first step, the collected straws are naturally dried, and the moisture content of the straws is 30%;|in the second step, a straw pulverizer is adopted to pulverize the collected straws, and the straw pulverizer is started to idle for 2-3 minutes before pulverization, so that the straw pulverizer is carried out after no abnormal phenomenon exists;|in the third step, a briquetting machine is adopted to carry out briquetting operation on the crushed straws, the briquetting efficiency is 0.1 ton/hour, and the power is 15 kilowatts;|in the fourth step, compressed agricultural straws are dried by hot air, and the moisture content of the straws is reduced to below 2%, so that living environment is not created for microorganisms, and the straws are not decomposed;|selecting a proper sealing place, wherein the sealing place is required to have a stable geological structure, a geological layer is dense, bare land, grassland and forest land can be selected for excavation, or a mined pit can be directly utilized for sealing, and then a downstream area with the flow direction of groundwater flow is selected to be far away from a water source, a living area and other protection areas;|in the sixth step, a pit for landfill is excavated, the excavation depth is 100-400 m below the ground, the bottom and four walls of the pit are reinforced and impervious by a curing layer, and the excavation area is not more than 100m 2 In order to prevent the ground from sinking, paving a layer of 60 cm-100 cm of the straws pretreated in the first step-the fifth step, paving a layer of quicklime on each layer of straws, compacting and reinforcing, wherein the paving height is not more than 100m below the ground, and the periphery of the layer of straws is covered by a curing layer;|the main components of the solidified layer are: 25-55% of mineral powder, 25-55% of silicate cement clinker, 4-10% of adhesion promoter, 2-8% of lime, 2-8% of anhydrite and 1-5% of active magnesium oxide in percentage by mass. (CN115504757)|TECHNICAL FIELD|[0001] The invention relates to the technical field of carbon emission reduction, in particular to a method for sealing and solidifying carbon by agricultural straws.|BACKGROUND ART|[0002] The existing carbon emission reduction technology is mainly divided into CO 2 Four links of capturing, transporting, utilizing and sealing, wherein the sealing main body is CO 2 Either gaseous or liquid, has low technical cost and risk of leakage.|[0003] On the other hand, after the agricultural straws are forbidden to be burnt by governments in various places, the agricultural straws are mainly divided into two main treatment modes, namely, the agricultural straws are directly returned to the field to enhance the soil fertility, and the agricultural straws are comprehensively utilized. Comprehensive utilization is divided into five categories of fuelling, fertilizer, feed, raw material and base material, and straw biomass is processed into different available resources.|[0004] The plant can directly convert CO in the atmosphere 2 Absorbing and converting the organic carbon compound into the agricultural straw as the waste, if the agricultural straw is not treated, decomposing the agricultural straw by microorganisms, re-entering carbon circulation, returning to the atmosphere, if the agricultural straw is comprehensively utilized, possibly obtaining certain environmental and economic benefits, but comprehensively utilizing the agricultural strawThe carbon emission is increased due to a large amount of energy consumption, and after comprehensive utilization, carbon elements fixed by the agricultural straw still return to carbon circulation, so that effective carbon emission reduction cannot be realized.|[0005] In summary, carbon emission reduction technology needs to be innovated, and the problem of processing agricultural straws needs to be solved better.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to solve the technical innovation of carbon emission reduction and the problems of agricultural straw treatment, and designs a method for sealing and storing agricultural straw and fixing carbon.|[0007] The technical scheme for achieving the purpose is that the method for sealing and storing carbon by using the agricultural straw comprises the following steps:|[0008] step one: collecting straws;|[0009] step two: crushing straw;|[0010] step three: compressing straw;|[0011] step four: drying operation;|[0012] step five: curing and sealing operation;|[0013] step six: and (5) reclamation backfilling operation.|[0014] As a further description of the technical scheme, in the first step, the collected straw is naturally dried, and the water content of the straw is about 30%.|[0015] As further description of the technical scheme, in the second step, the straw pulverizer is adopted to pulverize the collected straws, and the straw pulverizer is started to idle for 2-3 minutes before pulverization, so that the straw pulverizer is carried out after no abnormal phenomenon.|[0016] As a further description of the technical scheme, in the third step, a briquetting machine is adopted to carry out briquetting operation on the crushed straws, the briquetting efficiency is 0.1 ton/hour, and the power is 15 kilowatts.|[0017] As a further description of the technical scheme, in the fourth step, compressed agricultural straw is dried by hot air, so that the water content of the straw is reduced to below 2%, and living environment is prevented from being created for microorganisms so as to decompose the straw.|[0018] In the fifth step, a suitable sealing place is selected, the sealing place is required to have a stable geological structure and a dense geological layer, bare land, grassland and forest land can be selected for excavation, or the exploited pit can be directly utilized for sealing, and the downstream area of the groundwater flow direction is generally selected to be far away from a water source, a living area and other protection areas.|[0019] As a further description of the technical scheme, in the step six, the pit for landfill is excavated, the excavation depth is 100-400 m under the ground, the bottom and four walls of the pit are reinforced and impermeable by the solidified layers, and the excavation area is not more than 100m 2 In order to prevent the ground from sinking, paving a layer of 60 cm-100 cm of the straw pretreated in the first step and the fifth step, paving a layer of quicklime on each layer of straw, compacting and reinforcing, wherein the paving height is not more than 100m below the ground, and the periphery of the straw is covered by a curing layer.|[0020] As a further description of the present technical solution, the cured layer comprises the following main components: 25-55% of mineral powder, 25-55% of silicate cement clinker, 4-10% of adhesion promoter, 2-8% of lime, 2-8% of anhydrite and 1-5% of active magnesium oxide in percentage by mass.|[0021] The invention has the beneficial effects that 1. The invention directly seals the agricultural straw, the straw is derived from the agricultural waste, the cost is low and the straw is easy to obtain, and meanwhile, the respiration of the agricultural straw has the CO effect 2 The trapping action of the device is completed, so that the energy consumption is reduced, the carbon emission is reduced, and the economic cost is further reduced.|[0022] 2. The straw is harmless to the environment, the chemical property of the solidified layer is stable, the pollution to the surrounding soil is avoided, the structure of the solidified layer is stable, geological accidents are not easy to happen, and the solid straw is sealed compared with the gaseous or liquid CO 2 More green and safe without risk.|[0023] 3. According to the invention, the agricultural straw is directly sealed, the moisture is reduced, the microorganisms are reduced, the environment where the microorganisms are unsuitable for survival is created as much as possible, so that the microorganisms are prevented from decomposing the straw, the solidified layer plays a physical isolation role, and the carbon fixed by the agricultural straw is blocked from entering the carbon circulation, so that the long-term stable sealing effect is achieved, and the carbon emission reduction purpose is realized.|[0024] 4. Because the method has deeper land, stable structure and backfill after sealing, the original functions of the land can be recovered, and the land resources are not greatly occupied.|[0025] 5. Meanwhile, the sealing and carbon fixation of the agricultural straws also reduces the agricultural wastes and solves the treatment problem.|INVENTION MODE|Detailed Description|[0026] Firstly, the design of the invention is initially described, on one hand, the prior carbon emission reduction technology has lower cost performance and leakage risk. On the other hand, the plants can directly absorb and convert CO2 in the atmosphere into organic carbon compounds, the existing treatment mode of the agricultural straw serving as waste has the defects that the effective carbon emission reduction cannot be realized, the carbon emission reduction technology needs to be innovated, and the treatment problem of the agricultural straw needs to be better solved, so the invention designs a method for sealing and storing the agricultural straw and fixing the carbon.|[0027] The invention will be described in detail below, and a method for sealing and fixing carbon by using agricultural straw is characterized by comprising the following steps:|[0028] step one: collecting straws; in the first step, the collected straws are naturally dried, and the moisture content of the straws is about 30 percent.|[0029] Step two: crushing straw; in the second step, the straw pulverizer is adopted to pulverize the collected straws, and the straw pulverizer is started to idle for 2-3 minutes before pulverization, so that the straw pulverizer is carried out after no abnormal phenomenon exists.|[0030] Step three: compressing straw; in the third step, a briquetting machine is adopted to carry out briquetting operation on the crushed straws, the briquetting efficiency is 0.1 ton/hour, and the power is 15 kilowatts.|[0031] Step four: drying operation; in the fourth step, the compressed agricultural straw is dried by hot air, so that the water content of the straw is reduced to below 2%, and living environment is prevented from being created for microorganisms so as to decompose the straw.|[0032] Step five: curing and sealing operation; in the fifth step, a proper sealing place is selected, the sealing place is required to have a stable geological structure, a geological layer is dense, bare land, grassland and woodland can be selected for excavation, or a pit after exploitation can be directly utilized for sealing, and then a downstream area with the flow direction of groundwater flow is generally selected far away from a water source, a living area and other protection areas.|[0033] Step six: in the sixth step, a pit for landfill is excavated, the excavation depth is 100-400 m under the ground, the bottom and four walls of the pit are reinforced and impervious by a solidified layer, and the excavation area is not more than 100m 2 In order to prevent the ground from sinking, laying a layer of 60 cm-100 cm of pretreated straw in the first step, laying a layer of quicklime on each layer of straw, compacting and reinforcing the layer of quicklime, wherein the laying height is not more than 100m below the ground, the periphery of the layer of straw is covered by a curing layer, and the curing layer comprises the following main components: 25-55% of mineral powder, 25-55% of silicate cement clinker, 4-10% of adhesion promoter, 2-8% of lime, 2-8% of anhydrite and 1-5% of active magnesium oxide in percentage by mass.|[0034] The paving of the quicklime has the following functions:|[0035] (1) the quicklime absorbs moisture to form slaked lime, so that the quicklime plays a role of a drying agent;|[0036] (2) when the slaked lime is generated, huge heat is released, and the slaked lime is calcium hydroxide and alkaline, so that the slaked lime has the effects of disinfection and sterilization, reduces microorganisms and can prevent straw from decomposing;|[0037] (3) hardening and agglomerating the quicklime after absorbing water to achieve the effect of solidification and stabilization;|[0038] (4) the quicklime and the slaked lime can absorb carbon dioxide in the air to form calcium carbonate, so as to achieve the effect of carbon fixation.|[0039] After several years of sealing, even if there is CO 2 Gas generation but ambient solidified layer versus CO 2 The absorption effect can effectively prevent CO2 from escaping into the atmosphere, after the sealing is finished, the soil is covered and backfilled in time, different reclamation backfilling schemes are adopted according to different geological conditions and different damage degrees, ecological restoration is carried out, and the original functions of the land are not damaged, so that the land is returned to the land owner.|[0040] 1. The invention directly seals the agricultural straw, the straw is derived from the agricultural waste, the cost is low and the straw is easy to obtain, and simultaneously, the respiration of the agricultural straw has the CO effect 2 The trapping action of the carbon dioxide is completed, so that the energy consumption is reduced and the carbon emission is reducedAnd the economic cost is further reduced.|[0041] 2. The straw is harmless to the environment, the chemical property of the solidified layer is stable, the pollution to the surrounding soil is avoided, the structure of the solidified layer is stable, geological accidents are not easy to happen, and the solid straw is sealed compared with the gaseous or liquid CO 2 More green and safe without risk.|[0042] 3. According to the invention, the agricultural straw is directly sealed, the moisture is reduced, the microorganisms are reduced, the environment where the microorganisms are unsuitable for survival is created as much as possible, so that the microorganisms are prevented from decomposing the straw, the solidified layer plays a physical isolation role, and the carbon fixed by the agricultural straw is blocked from entering the carbon circulation, so that the long-term stable sealing effect is achieved, and the carbon emission reduction purpose is realized.|[0043] 4. Because the method has deeper land, stable structure and backfill after sealing, the original functions of the land can be recovered, and the land resources are not greatly occupied.|[0044] 5. Meanwhile, the sealing and carbon fixation of the agricultural straws also reduces the agricultural wastes and solves the treatment problem.|[0045] The invention solves the problem of processing the agricultural straws on one hand, realizes low-cost carbon emission reduction on the other hand, is safe and pollution-free, has extremely high cost performance and can be popularized and applied on a large scale.|[0046] The above technical solution only represents the preferred technical solution of the present invention, and some changes that may be made by those skilled in the art to some parts of the technical solution represent the principles of the present invention, and the technical solution falls within the scope of the present invention. (CN115504757)|TECHNICAL FIELD|[0001] The invention relates to the technical field of carbon emission reduction, in particular to a method for sealing and solidifying carbon by agricultural straws.|BACKGROUND ART|[0002] The existing carbon emission reduction technology is mainly divided into CO 2 Four links of capturing, transporting, utilizing and sealing, wherein the sealing main body is CO 2 Either gaseous or liquid, has low technical cost and risk of leakage.|[0003] On the other hand, after the agricultural straws are forbidden to be burnt by governments in various places, the agricultural straws are mainly divided into two main treatment modes, namely, the agricultural straws are directly returned to the field to enhance the soil fertility, and the agricultural straws are comprehensively utilized. Comprehensive utilization is divided into five categories of fuelling, fertilizer, feed, raw material and base material, and straw biomass is processed into different available resources.|[0004] The plant can directly convert CO in the atmosphere 2 Absorbing and converting the organic carbon compound into the agricultural straw as the waste, if the agricultural straw is not treated, decomposing the agricultural straw by microorganisms, re-entering carbon circulation, returning to the atmosphere, if the agricultural straw is comprehensively utilized, possibly obtaining certain environmental and economic benefits, but comprehensively utilizing the agricultural strawThe carbon emission is increased due to a large amount of energy consumption, and after comprehensive utilization, carbon elements fixed by the agricultural straw still return to carbon circulation, so that effective carbon emission reduction cannot be realized.|[0005] In summary, carbon emission reduction technology needs to be innovated, and the problem of processing agricultural straws needs to be solved better.|DISCLOSURE|Disclosure of Invention|[0006] The invention aims to solve the technical innovation of carbon emission reduction and the problems of agricultural straw treatment, and designs a method for sealing and storing agricultural straw and fixing carbon.|[0007] The technical scheme for achieving the purpose is that the method for sealing and storing carbon by using the agricultural straw comprises the following steps:|[0008] step one: collecting straws;|[0009] step two: crushing straw;|[0010] step three: compressing straw;|[0011] step four: drying operation;|[0012] step five: curing and sealing operation;|[0013] step six: and (5) reclamation backfilling operation.|[0014] As a further description of the technical scheme, in the first step, the collected straw is naturally dried, and the water content of the straw is about 30%.|[0015] As further description of the technical scheme, in the second step, the straw pulverizer is adopted to pulverize the collected straws, and the straw pulverizer is started to idle for 2-3 minutes before pulverization, so that the straw pulverizer is carried out after no abnormal phenomenon.|[0016] As a further description of the technical scheme, in the third step, a briquetting machine is adopted to carry out briquetting operation on the crushed straws, the briquetting efficiency is 0.1 ton/hour, and the power is 15 kilowatts.|[0017] As a further description of the technical scheme, in the fourth step, compressed agricultural straw is dried by hot air, so that the water content of the straw is reduced to below 2%, and living environment is prevented from being created for microorganisms so as to decompose the straw.|[0018] In the fifth step, a suitable sealing place is selected, the sealing place is required to have a stable geological structure and a dense geological layer, bare land, grassland and forest land can be selected for excavation, or the exploited pit can be directly utilized for sealing, and the downstream area of the groundwater flow direction is generally selected to be far away from a water source, a living area and other protection areas.|[0019] As a further description of the technical scheme, in the step six, the pit for landfill is excavated, the excavation depth is 100-400 m under the ground, the bottom and four walls of the pit are reinforced and impermeable by the solidified layers, and the excavation area is not more than 100m 2 In order to prevent the ground from sinking, paving a layer of 60 cm-100 cm of the straw pretreated in the first step and the fifth step, paving a layer of quicklime on each layer of straw, compacting and reinforcing, wherein the paving height is not more than 100m below the ground, and the periphery of the straw is covered by a curing layer.|[0020] As a further description of the present technical solution, the cured layer comprises the following main components: 25-55% of mineral powder, 25-55% of silicate cement clinker, 4-10% of adhesion promoter, 2-8% of lime, 2-8% of anhydrite and 1-5% of active magnesium oxide in percentage by mass.|[0021] The invention has the beneficial effects that 1. The invention directly seals the agricultural straw, the straw is derived from the agricultural waste, the cost is low and the straw is easy to obtain, and meanwhile, the respiration of the agricultural straw has the CO effect 2 The trapping action of the device is completed, so that the energy consumption is reduced, the carbon emission is reduced, and the economic cost is further reduced.|[0022] 2. The straw is harmless to the environment, the chemical property of the solidified layer is stable, the pollution to the surrounding soil is avoided, the structure of the solidified layer is stable, geological accidents are not easy to happen, and the solid straw is sealed compared with the gaseous or liquid CO 2 More green and safe without risk.|[0023] 3. According to the invention, the agricultural straw is directly sealed, the moisture is reduced, the microorganisms are reduced, the environment where the microorganisms are unsuitable for survival is created as much as possible, so that the microorganisms are prevented from decomposing the straw, the solidified layer plays a physical isolation role, and the carbon fixed by the agricultural straw is blocked from entering the carbon circulation, so that the long-term stable sealing effect is achieved, and the carbon emission reduction purpose is realized.|[0024] 4. Because the method has deeper land, stable structure and backfill after sealing, the original functions of the land can be recovered, and the land resources are not greatly occupied.|[0025] 5. Meanwhile, the sealing and carbon fixation of the agricultural straws also reduces the agricultural wastes and solves the treatment problem.|INVENTION MODE|Detailed Description|[0026] Firstly, the design of the invention is initially described, on one hand, the prior carbon emission reduction technology has lower cost performance and leakage risk. On the other hand, the plants can directly absorb and convert CO2 in the atmosphere into organic carbon compounds, the existing treatment mode of the agricultural straw serving as waste has the defects that the effective carbon emission reduction cannot be realized, the carbon emission reduction technology needs to be innovated, and the treatment problem of the agricultural straw needs to be better solved, so the invention designs a method for sealing and storing the agricultural straw and fixing the carbon.|[0027] The invention will be described in detail below, and a method for sealing and fixing carbon by using agricultural straw is characterized by comprising the following steps:|[0028] step one: collecting straws; in the first step, the collected straws are naturally dried, and the moisture content of the straws is about 30 percent.|[0029] Step two: crushing straw; in the second step, the straw pulverizer is adopted to pulverize the collected straws, and the straw pulverizer is started to idle for 2-3 minutes before pulverization, so that the straw pulverizer is carried out after no abnormal phenomenon exists.|[0030] Step three: compressing straw; in the third step, a briquetting machine is adopted to carry out briquetting operation on the crushed straws, the briquetting efficiency is 0.1 ton/hour, and the power is 15 kilowatts.|[0031] Step four: drying operation; in the fourth step, the compressed agricultural straw is dried by hot air, so that the water content of the straw is reduced to below 2%, and living environment is prevented from being created for microorganisms so as to decompose the straw.|[0032] Step five: curing and sealing operation; in the fifth step, a proper sealing place is selected, the sealing place is required to have a stable geological structure, a geological layer is dense, bare land, grassland and woodland can be selected for excavation, or a pit after exploitation can be directly utilized for sealing, and then a downstream area with the flow direction of groundwater flow is generally selected far away from a water source, a living area and other protection areas.|[0033] Step six: in the sixth step, a pit for landfill is excavated, the excavation depth is 100-400 m under the ground, the bottom and four walls of the pit are reinforced and impervious by a solidified layer, and the excavation area is not more than 100m 2 In order to prevent the ground from sinking, laying a layer of 60 cm-100 cm of pretreated straw in the first step, laying a layer of quicklime on each layer of straw, compacting and reinforcing the layer of quicklime, wherein the laying height is not more than 100m below the ground, the periphery of the layer of straw is covered by a curing layer, and the curing layer comprises the following main components: 25-55% of mineral powder, 25-55% of silicate cement clinker, 4-10% of adhesion promoter, 2-8% of lime, 2-8% of anhydrite and 1-5% of active magnesium oxide in percentage by mass.|[0034] The paving of the quicklime has the following functions:|[0035] (1) the quicklime absorbs moisture to form slaked lime, so that the quicklime plays a role of a drying agent;|[0036] (2) when the slaked lime is generated, huge heat is released, and the slaked lime is calcium hydroxide and alkaline, so that the slaked lime has the effects of disinfection and sterilization, reduces microorganisms and can prevent straw from decomposing;|[0037] (3) hardening and agglomerating the quicklime after absorbing water to achieve the effect of solidification and stabilization;|[0038] (4) the quicklime and the slaked lime can absorb carbon dioxide in the air to form calcium carbonate, so as to achieve the effect of carbon fixation.|[0039] After several years of sealing, even if there is CO 2 Gas generation but ambient solidified layer versus CO 2 The absorption effect can effectively prevent CO2 from escaping into the atmosphere, after the sealing is finished, the soil is covered and backfilled in time, different reclamation backfilling schemes are adopted according to different geological conditions and different damage degrees, ecological restoration is carried out, and the original functions of the land are not damaged, so that the land is returned to the land owner.|[0040] 1. The invention directly seals the agricultural straw, the straw is derived from the agricultural waste, the cost is low and the straw is easy to obtain, and simultaneously, the respiration of the agricultural straw has the CO effect 2 The trapping action of the carbon dioxide is completed, so that the energy consumption is reduced and the carbon emission is reducedAnd the economic cost is further reduced.|[0041] 2. The straw is harmless to the environment, the chemical property of the solidified layer is stable, the pollution to the surrounding soil is avoided, the structure of the solidified layer is stable, geological accidents are not easy to happen, and the solid straw is sealed compared with the gaseous or liquid CO 2 More green and safe without risk.|[0042] 3. According to the invention, the agricultural straw is directly sealed, the moisture is reduced, the microorganisms are reduced, the environment where the microorganisms are unsuitable for survival is created as much as possible, so that the microorganisms are prevented from decomposing the straw, the solidified layer plays a physical isolation role, and the carbon fixed by the agricultural straw is blocked from entering the carbon circulation, so that the long-term stable sealing effect is achieved, and the carbon emission reduction purpose is realized.|[0043] 4. Because the method has deeper land, stable structure and backfill after sealing, the original functions of the land can be recovered, and the land resources are not greatly occupied.|[0044] 5. Meanwhile, the sealing and carbon fixation of the agricultural straws also reduces the agricultural wastes and solves the treatment problem.|[0045] The invention solves the problem of processing the agricultural straws on one hand, realizes low-cost carbon emission reduction on the other hand, is safe and pollution-free, has extremely high cost performance and can be popularized and applied on a large scale.|[0046] The above technical solution only represents the preferred technical solution of the present invention, and some changes that may be made by those skilled in the art to some parts of the technical solution represent the principles of the present invention, and the technical solution falls within the scope of the present invention. Family Number|(103140257)|103140257|Abstract|(CN115504757B B)|The invention discloses an agricultural straw sealing and carbon sequestration method . The method comprises the following steps : step 1, straw collection ; step 2, straw crushing operation ; step 3, straw compression operation ; step 4, drying operation ; 5, curing and sealing operation ; and 6, carrying out reclamation backfill operation . The method has the advantages that the agricultural straw is directly sealed and stored , the straw is derived from agricultural waste and is low in price and easy to obtain , meanwhile , CO2 trapping action is completed through respiration of the agricultural straw , energy consumption is reduced , carbon emission is reduced , the economic cost is further reduced , the straw is harmless to the environment , the chemical property of a solidified layer is stable , and the method is suitable for industrial production . In addition , the solidified layer is stable in structure , geological accidents are not prone to being caused , and sealed solid straw is greener , safer and risk - free than sealed gaseous or liquid CO2 . |CPC codes|(CN115504757B B)|B01D - 053/62 |B01D - 053/85 |B01D - 2257/504 |IPC codes|(CN115504757B B)|B01D - 053/62 |B01D - 053/85 |Title|(CN115504757 A)|Method for sequestration and carbon sequestration of agricultural straws | Environmental technology|Materials, metallurgy B01D-053/62|B01D-053/85|B01D-2257/504|C04B-028/16|C04B-2111/00732 (GR1) C04B-028/16[RK1]; C04B-018/12[RK2]; C04B-007/02[RK3]; C04B-022/06/4[RK4]; C04B-022/06/6[RK5] B01D-053/62|B01D-053/85|B01D-2257/504|C04B-028/16|C04B-2111/00732 B01D-053/62|B01D-053/85|C04B-028/16 B01D-053/62|B01D-053/85|C04B-028/16 CN114426419|CN108570482|CN107094444|CN104891878|CN103229653|CN103155776|US20110038774|CN101224464 CN114426419 99868789 WHO=Examiner SELF=N|CN108570482 81406540 WHO=Examiner SELF=N|CN107094444 77104297 WHO=Examiner SELF=N|CN104891878 70805604 WHO=Examiner SELF=N|CN103229653 45748470 WHO=Examiner SELF=N|CN103155776 45464871 WHO=Examiner SELF=N|US20110038774 7239128 WHO=Examiner SELF=N|CN101224464 62146299 WHO=Examiner SELF=N CN101224464; CN104891878; CN103155776; CN103229653; CN107094444; CN108570482; CN114426419; US20110038774 GRANTED (CN115504757)|GRANTED ALIVE (CN115504757)|ALIVE (CN115504757)|LEGAL DETAILS FOR CN115504757|Actual or expected expiration date=2042-09-27|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-09-27|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211188508|Application date=2022-09-27|Standardized application number=2022CN-1188508|Event publication date=2022-12-23|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115504757|Publication stage code=A|Publication date=2022-12-23|Standardized publication number=CN115504757|Event publication date=2022-12-23|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-01-10|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-10-03|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN115504757|Publication stage code=B|Publication date=2023-10-03|Standardized publication number=CN115504757B|Event publication date=2023-10-03|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN115504757)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSqVUuy+5ODdhj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=VsjlIZrCrV1kRySu7MjW1LmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN115504757)|CN|(CN115504757)|CN (CN115504757)|NAME=DONGGUAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN|(CN115504757)|NAME=DONGGUAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN115504757)|NAME=XU YONGLEI;SUZHOU YANSIJIAXIN PATENT AGENCY (GENERAL PARTNERSHIP) , REG=32385|(CN115504757)|NAME=XU YONGLEI;SUZHOU YANSIJIAXIN PATENT AGENCY (GENERAL PARTNERSHIP) , REG=32385 (CN115504757)|NAME=HUANG XIA|NAME=YU CHUNXUE|NAME=ZHENG YUANHUAN|NAME=SU MEIRONG|NAME=HOU XIAOSHU|(CN115504757)|NAME=HUANG XIA|NAME=YU CHUNXUE|NAME=ZHENG YUANHUAN|NAME=SU MEIRONG|NAME=HOU XIAOSHU 0 1 Titre: (CN115504757)|Method for sealing and carbon fixation of agricultural straw Résumé: (CN115504757)|The invention discloses an agricultural straw sealing and carbon sequestration method. The method comprises the following steps: step 1, straw collection; step 2, straw crushing operation; step 3, straw compression operation; step 4, drying operation; 5, curing and sealing operation; and 6, carrying out reclamation backfill operation. The method has the advantages that the agricultural straw is directly sealed and stored, the straw is derived from agricultural waste and is low in price and easy to obtain, meanwhile, CO2 trapping action is completed through respiration of the agricultural straw, energy consumption is reduced, carbon emission is reduced, the economic cost is further reduced, the straw is harmless to the environment, the chemical property of a solidified layer is stable, and the method is suitable for industrial production. In addition, the solidified layer is stable in structure, geological accidents are not prone to being caused, and sealed solid straw is greener, safer and risk-free than sealed gaseous or liquid CO2. 71 Abstract gpt-4o-mini no The method focuses on sealing and storing agricultural straw for carbon sequestration, without involving mineral weathering or CO₂ capture through mineral carbonation.
72 US63/230,843P|US63/230,843|US17/705,792 CA3191648|ZA202208785|JP2022121235|AU2022209209|EP22175231|ES22175231T|AEP6000645/2022|US17/705,792 ES2997244|AEP6000645/2022|US12168610|ZA202208785|EP4134513|EP4134513|JP7384477|CA3191648|AU2022209209|JP2023024948|EP4134513|US20230038447 103686458 CA3191648 A1 2023-09-28 [CA3191648]|ZA202208785 B 2024-09-25 [ZA202208785]|JP7384477 B2 2023-11-21 [JP7384477]|JP2023024948 A 2023-02-21 [JP2023024948]|AU2022209209 A1 2023-02-23 [AU2022209209]|EP4134513 B1 2024-08-07 [EP4134513]|EP4134513 C0 2024-08-07 [EP4134513]|EP4134513 A1 2023-02-15 [EP4134513]|ES2997244 T3 2025-02-14 [ES2997244]|AEP6000645/2022 A1 2024-12-17 [AE20226000645]|US12168610 B2 2024-12-17 [US12168610]|US20230038447 A1 2023-02-09 [US20230038447] 2021-08-09|2022-03-28 2023-03-02|2022-08-05|2022-07-29|2022-07-25|2022-05-24|2022-05-24|2022-04-11|2022-03-28 2025-02-14|2024-12-17|2024-12-17|2024-09-25|2024-08-07|2024-08-07|2023-11-21|2023-09-28|2023-02-23|2023-02-21|2023-02-15|2023-02-09 (EP4134513)|2024-08-07|(US12168610)|2024-12-17|(JP7384477)|2023-11-21|(ES2997244)|2025-02-14|(ZA202208785)|2024-09-25||| (EP4134513)|2042-05-24|(US12168610)|2042-03-28|(JP7384477)|2042-07-29|(ES2997244)|2042-05-24|(ZA202208785)|2042-08-05|(AEP6000645/2022)|2042-04-11|(CA3191648)|2043-03-02|(AU2022209209)|2042-07-25 (EP4134513)|System and method for permanent carbon dioxide sequestration using a renewable energy source (EP4134513)|Here is provided a system and method to mineralize CO2 into peridotite rock formations in situ in a controlled and efficient manner removing carbon permanently from the atmosphere. Carbon dioxide sequestration into peridotite rocks happens naturally by means of natural weathering. This process is slow and might take thousands of years to transform considerable amount of CO2 into carbonate rocks. The present method disclosed herein shortens the time of mineralization considerably in a controlled and quantifiable manner. This is typically done by injecting CO2 into peridotite rock formation and creating efficient reaction pathways and conditions for the mineralization reaction to happen and therefore store CO2 by conversion into magnesite (MgCO3) and calcite (CaCO3). PROTOSTAR GROUP (EP4134513)|PROTOSTAR GROUP LIMITED|(EP4134513)|PROTOSTAR GROUP LIMITED ([GB])|(EP4134513)|PROTOSTAR GROUP LIMITED ([GB])|(US12168610)|Protostar Group Ltd. ([GB])|(US20230038447)|Protostar Group Ltd. ([GB])|(JP7384477)|PROTOSTAR GROUP LTD|(JP2023024948)|PROTOSTAR GROUP LTD|(ES2997244)|PROTOSTAR GROUP LIMITED|(ZA202208785)|PROTOSTAR GROUP LTD.|(AEP6000645/2022)|Protostar Group Ltd ([GB])|(CA3191648)|PROTOSTAR GROUP LTD. ([GB])|(AU2022209209)|PROTOSTAR GROUP LTD. HASAN TALAL|KHIMJI KARAN|TASFAI EHAB (EP4134513)|HASAN, Talal|KHIMJI, Karan|TASFAI, Ehab|(EP4134513)|HASAN, Talal|KHIMJI, Karan|TASFAI, Ehab|(EP4134513)|PROTOSTAR GROUP LIMITED (EP4134513)|Kransell & Wennborg KB ([SE])|Reg. Nb: 101410948|(US12168610)|Oblon, McClelland, Maier & Neustadt, L.L.P.|(JP7384477)|SUZUYE & SUZUYE|Reg. Nb: 110003708|KURATA, Masatoshi et al.|Reg. Nb: 100108855|INOUE, Tadashi|Reg. Nb: 100179062|KYOKUTO RESIN:KK|Reg. Nb: 100199565|Naoyuki Yato|Reg. Nb: 100212705|Ikuharu Ohya|Reg. Nb: 100219542|KONO NAOKI|Reg. Nb: 100153051|KANEKO SANAE|Reg. Nb: 100162570|(AEP6000645/2022)|Dennemeyer and Associates S A ([AE])|Reg. Nb: 704210|(CA3191648)|GOWLING WLG (CANADA) LLP ([CA])|(AU2022209209)|Pizzeys Patent and Trade Mark Attorneys Pty Ltd ([AU]) (EP4134513)|It is then advantageous to seal the return fluid well (for example by cementing) and relocate injection of the CO2 rich fluid-mixture to an injection point located differently than an initial well.|The present disclosure provides an efficient and controlled method for CO2 mineralization into peridotite rocks using renewable energy.|This whole process is advantageously powered by a hybrid-renewable system to keep a carbon footprint low and maximize the net amount of CO2 eliminated (see section 2 below).|For the most part, because of the requirements for heating and processing, these approaches have been found to be too expensive in financial terms and, more importantly, in energy expenditure, not commercially viable at present.|Gas flow is difficult to regulate due to the impact of temperature upstream and downstream pressure on the flow rate.| (EP4134513)|1. A method of carbon dioxide sequestration by in situ mineralization characterized in that: an amount of carbon dioxide is dissolved into water to form a carbon dioxide and water mixture; an amount of said carbon dioxide and water mixture is injected into a rock formation comprising peridotite via an injection well (220, 320, 1020), wherein the carbon dioxide and water mixture is flowed through said injection well having a non-corrosive well casing and a non-corrosive injection well tubing disposed in the rock formation, and at least one packer creating a packed off interval, said injection well tubing having a plurality of longitudinal perforations at a depth of 0.4 to 4 km in said rock formation; a high-pressure zone is created within said injection well (220, 320, 1020) below said packed off interval, water from said rock formation is recycled via an observation well (230, 330, 1030) creating a low-pressure zone during said recycling through the observation well (230, 330, 1030). ; carbon dioxide in said carbon dioxide and water mixture is reacted with said rock formation to form calcites and magnesites, and all steps of the process are powered by a renewable energy source.|9. A system for controlled enhancement of peridotite in situ mineralization characterized in that said system comprises: an injection well (220, 320, 1020) bored in a rock formation comprising peridotite and having a non-corrosive well casing; a non-corrosive injection well tubing disposed in said injection well; a packer module (312, 1012) connected to the injection tubing and disposed in the injection well; a renewable energy source; a gas dissolution module (310) connected to the renewable energy source, wherein the gas dissolution module includes a carbon dioxide and water mixture ejection port, and wherein all steps are powered by the renewable energy source.| (EP4134513)|A first aspect relates to a method of carbon dioxide sequestration by in situ mineralization comprising the steps of dissolving an amount of carbon dioxide into water to form a carbon dioxide and water mixture; injecting an amount of said carbon dioxide and water mixture into a rock formation comprising peridotite via an injection well, wherein the carbon dioxide and water mixture is flowed through the injection well or an injection well tubing disposed in the rock formation, the injection well and/or injection well tubing having a plurality of longitudinal perforations at a depth of 0.4 to 4 km in the rock formation; recycling water from said rock formation via an observation well; and reacting carbon dioxide in said carbon dioxide and water mixture with said rock formation to form calcites and magnesites, and all steps of the process are powered by a renewable energy source.|A second aspect relates to a system for controlled enhancement of peridotite in situ mineralization, comprising: an injection well bored in a rock formation and having a non-corrosive well casing; a non-corrosive injection well tubing disposed in the injection well; a packer module connected to the injection tubing and disposed in the injection well; a renewable energy source; a gas dissolution module connected to the renewable energy source, wherein the gas dissolution module includes a carbon dioxide and water mixture ejection port, and wherein all steps are powered by a renewable energy source.|The present disclosure relates to a system and method for permanent carbon dioxide (CO2) sequestration in peridotite rock formations. More specifically, the present disclosure relates to accelerating and controlling natural peridotite carbonation between peridotite and a source of carbon dioxide to be sequestered. The present disclosure also relates to methods for permanently sequestering carbon dioxide that is captured from industrial emissions, atmospheric air, or that contained in bodies of fluid. The present disclosure also relates to the use of renewable sources of energy for carbon capture plants and carbon storage process equipment.| (US12168610)|CARBON DIOXIDE(100,62)|CARBON DIOXIDE SEQUESTRATION(100,11)|RENEWABLE ENERGY SOURCE(100,8)|UNDERGROUND GEOLOGICAL FORMATION(100,3)|IN SITU MINERALIZATION(100,2)|GEOLOGICAL FORMATION(99,29)|PERIDOTITE ROCK(66,6)|TUBING(57,11)|INJECTED CARBON DIOXIDE(52,3)|CASING CEMENTATION(51,2)|SYNCHRONIZED BIOFUEL GENERATOR(51,1)|MAGNESITE(47,5)|MINIMAL INTERRUPTION(46,1)|GEOLOGICAL FORMATION MINIMUM DEPTH(44,2)|PERFORATION(41,14)|GAS DISSOLUTION MODULE(41,9)|CALCITE(41,5)|BIO FUEL GENERATOR(41,4)|CO2 RICH INJECTION(39,5)|GEOLOGICAL FORMATION MAXIMUM DEPTH(39,2)|MINIMUM DEPTH(37,3)|RECYCLING WATER(37,2)|PERIDOTITE(36,16)|EVAPORATIVE COOLING(36,2)|FINANCIAL TERM(36,1)|NATURAL WEATHERING(36,1)|SOLAR INVERTER(36,1)|SUBSURFACE MODULE(35,1)|CO2 RICH(34,20)|SOLAR PHOTOVOLTAIC PANEL(32,1)|SERVICING(31,1)|PACKER(30,9)|CARBONATE ROCK(30,2)|MINERALIZATION REACTION(30,2)|BUBBLE DIAMETER(29,1)|CO2(26,40)|BIO FUEL ENERGY(26,1)|MAXIMUM DEPTH(25,6)|HYBRID RENEWABLE(24,2)|HYDROELECTRICITY(24,1)|REACTION PATHWAY(23,6)|GAS DISSOLUTION(23,2)|DOWNSTREAM PRESSURE(21,1)|INTERNAL ACCESS(21,1)|RETURN WELL(20,10)|PROJECT APPLICATION ACCOUNTING(20,1)|SOLAR ENERGY MODULE(20,1)|CARBON FOOTPRINT(19,1)|RETURN FLUID(17,9)|INJECTION BOREHOLE WELL HEAD(17,5)|PERIDOTITE VOLUME(15,7)|MGCO3(15,2)|CO2 DISSOLUTION(14,7)|CACO3(14,2)|GEOTHERMAL ENERGY(14,1)|SLOW FLOW VELOCITY(14,1)|MONITORING BOREHOLE(12,4)|WIND TURBINE(12,3)|INJECTION POINT(12,2)|PERIDOTITE RESERVOIR(12,2)|ARTIFICIAL CONSERVATIVE TRACER(12,1)|CARBON FOOTPRINT LOW(12,1)|DISSOLUTION RESIDENCE TIME(12,1)|GAS FLOW(12,1)|HYDRO ENERGY(12,1)|MINERALIZATION TIME(12,1)|INJECTION WELL(11,20)|MINIMUM TEMPERATURE(10,2)|RENEWABLE ENERGY STORAGE MODULE(10,2)|ESTIMATING CO2 MINERALIZATION CAPACITY(10,1)|HYBRID ENERGY SOURCE(10,1)|INJECTED CONSERVATIVE TRACER(10,1)|INJECTION BOREHOLE DEEP PERFORATION(10,1)|INJECTION BOREHOLE PERFORATION(10,1)|MAGNESIA PERIDOTITE ORE PRODUCTION(10,1)|NATURAL PERIDOTITE CARBONATION(10,1)|NONCORROSIVE CASING PERMANENT INSTALLATION(10,1)|OLIVINE CARBONATION(10,1)|PERFORATION CAREFUL PLACEMENT(10,1)|PERIDOTITE MINERALIZATION(10,1)|PERIDOTITE NATURAL CARBONATION(10,1)|PERIDOTITE REACTIVITY(10,1)|POLLUTANT REMEDIATION(10,1)|PYROXENE MINERAL LESSER PROPORTION(10,1)|SUBMERSIBLE PUMP(9,13)|TARGET INJECTION ZONE(9,4)|WATER MASS RATIO(9,3)|AMBIENT RESERVOIR GROUNDWATER(9,1)|FLOWING MIXTURE(9,1)|GREEN ENERGY SOURCE(9,1)|PERIDOTITE IGNEOUS ROCK(9,1)|RECOVERY BOREHOLE COLLECT(9,1)|SWITCH GEAR(9,1)|TECTONICALLY EXPOSED PERIDOTITE(9,1)|WIND ENERGY(9,1)|PACKER TOOL(8,2)|CO2 EFFERVESCENCE(8,1)|CO2 LATE INJECTION(8,1)|DEEP BOREHOLE(8,1)|DOWNHOLE INJECTION PIPING(8,1)|FIXATION CO2 ABSORPTION(8,1)|GLACIER RETREAT(8,1)|H2S ABATEMENT(8,1)|INJECTED CO2 RICH MONITORING(8,1)|INOSILICATE MINERAL(8,1)|MANTLE PERIDOTITE(8,1)|OBSERVED CLIMATE CHANGEOVER(8,1)|POLLUTANT SUPPRESSION(8,1)|RECONNAISSANCE MAPPING(8,1)|RECOVERING BOREHOLE(8,1)|RETURN FLUID WELL(8,1)|SENSITIVE THERMODYNAMIC BEHAVIOR(8,1)|SERPENTINE REACTANT(8,1)|SIZE GAS BUBBLE(8,1)|STANDBY WING(8,1)|SUBMERSIBLE INTAKE PUMP(8,1)|SUBSURFACE CONNECTIVITY(8,1)|CO2 MOLAR RATIO(7,3)|OLIVINE REACTION(7,2)|ABUNDANT MINERAL(7,1)|ANTHROPOGENIC IMPACT(7,1)|BUFFER TANK SIZING(7,1)|BULK ROCK FRACTURE STRESS(7,1)|CO2 COLLISION(7,1)|CO2 FIXATION DECREASE(7,1)|CO2 RICH RELEASE(7,1)|DARCY LAW(7,1)|DISSOLVED CO2 SOLUBILITY(7,1)|EARTH MANTLE(7,1)|FLUID RESIDENCE TIME(7,1)|GAS INFLATION PACKER(7,1)|GEOLOGICAL RESERVOIR(7,1)|GLOBAL WARMING SUPPRESSION(7,1)|HYDROUS ALTERATION PRODUCT(7,1)|INJECTION BOREHOLE WALL(7,1)|LIQUID CONSERVATIVE TRACER(7,1)|MAGNESIA PURITY(7,1)|MG CARBONATION(7,1)|MINERAL OLIVINE(7,1)|NONCORROSIVE PIPE(7,1)|OBSERVATION BOREHOLE FLUID(7,1)|OUTGOING SAMPLING PORT(7,1)|PERFORATION DEPTH(7,1)|PERIDOTITE PERMEABLE LAYER(7,1)|PERIDOTITE ROCK FORMATION(7,1)|POLYMER TUBING STRING(7,1)|PROGRAM REPORT(7,1)|RECOVERY BOREHOLE DEPTH(7,1)|SOLUBILIZED CO2(7,1)|SUPPRESSING GLOBAL WARMING(7,1)|UNINTERRUPTED CO2(7,1)|UNINTERRUPTED DRAW(7,1)|POROSITY(6,4)|FLUID INJECTION(6,3)|GAS FLOW RATE(6,3)|CO2 TANK(6,2)|PERIDOTITE LAYER(6,2)|TRACER FLUID(6,2)|ACCURATE ACCOUNTING(6,1)|BIO FUEL MODULE(6,1)|BOREHOLE FULL DEPTH(6,1)|BURNING FOSSIL FUEL(6,1)|CARBONATION REACTION(6,1)|CO2 EMISSION(6,1)|CONSEQUENTIAL DAMAGE SEQUESTRATION(6,1)|DILUTION CALCULATION(6,1)|DISSOLVED CO2 ANALYSIS(6,1)|DOMINANT INFLUENCE(6,1)|INJECTION PIPELINE(6,1)|INJECTION PORTABILITY(6,1)|LIVE MONITORING(6,1)|MAXIMIZE BUBBLE(6,1)|MONITORING OBSERVATION BOREHOLE(6,1)|NATURAL FRACTURE NETWORK(6,1)|NATURAL TRACER(6,1)|PAST CENTURY(6,1)|PAST DECADE(6,1)|PERIDOTITE GEOLOGIC FORMATION(6,1)|PERMANENTLY SEQUESTERING CARBON DIOXIDE(6,1)|PERMEABLE ZONE(6,1)|SEA FLOOR(6,1)|STABLE CARBONATE MINERAL(6,1)|SUBTERRANEAN GEOLOGIC FORMATION(6,1)|TARGET SETPOINT(6,1)|TRACER MOLAR RATIO(6,1)|TRACER SUBSTANCE(6,1)|UNDISSOLVED CO2 GAS BUBBLE(6,1)|PHOTOVOLTAIC(5,3)|ATMOSPHERIC CO2(5,2)|BLOCKAGE(5,2)|FINE POWDER(5,2)|H2S GAS BUBBLE(5,2)|INTERMITTENCY(5,2)|MG3SI2O(5,2)|PRETREATMENT(5,2)|REAGENT(5,2)|SEAWATER(5,2)|TARGET FORMATION(5,2)|BOOSTER PUMP(4,4)|DOSING PUMP(4,4)|MBGL(4,4)|AQUEOUS SOLUTION(4,3)|CARBONIC ACID(4,3)|PACKED OFF INTERVAL(4,3)|PRESSURIZED WATER STREAM(4,3)|RETURN FLUID PIPE(4,3)|DRILLING(4,2)|ABSORPTION ENHANCEMENT(4,1)|ACCELERATE REMOVAL(4,1)|ALTERATION NATURE(4,1)|ARTIFICIALLY PRODUCED CA(4,1)|ATMOSPHERIC CARBON DIOXIDE YEAR(4,1)|BOREHOLE SINGLE HEMISPHERE(4,1)|BUOYANCY(4,1)|CHEMICAL WEATHERING ACCELERATION(4,1)|CO2 EMITTING INDUSTRY(4,1)|CO2 PERIDOTITE REACTION(4,1)|CO2 PYROXENE REACTION(4,1)|CO2 STORAGE FACILITY(4,1)|DAMPENING PRESSURE FLUCTUATION(4,1)|FLUID FLOWPATH(4,1)|FOSSIL FUEL CONSUMPTION(4,1)|FUZED PHOSPHATE(4,1)|GEOLOGICAL FORMATION TARGET ZONE(4,1)|HOMOGENEOUS NATURE(4,1)|HYBRID CONTROLLER(4,1)|HYDRAULIC COMMUNICATION(4,1)|INCOMING INJECTION FLUID(4,1)|INJECTED FLUID HOMOGENOUS NATURE(4,1)|INJECTION ZONE INTERVAL(4,1)|INSTRUMENTALITY(4,1)|INTERMITTENT NATURE(4,1)|ISOLATED INJECTION INTERVAL(4,1)|LIMITING NATURAL FRACTURE(4,1)|MAGNESIUM SINKING PROCESSING(4,1)|MAGNETIC BEHAVIOR(4,1)|MONITORING MODULE(4,1)|NIGHT LOAD(4,1)|NONCORROSIVE FLUID PIPE(4,1)|OVERPRESSURE(4,1)|PERIDOTITE FORMATION ILLUSTRATION(4,1)|PERIDOTITE MAGNESIUM OXIDE(4,1)|PERIDOTITE MAXIMUM DEPTH(4,1)|PERMEABILITY TEST(4,1)|PLACEMENT DEPTH(4,1)|PRIMARY WING(4,1)|REMOVING IMPURITY(4,1)|RETURN BOREHOLE WALL(4,1)|SOLID CARBONATE MINERAL(4,1)|SUBSURFACE FORMATION(4,1)|TARGET INJECTION INTERVAL(4,1)|TREATING CO2(4,1)|UNDERGROUND ROCK FORMATION(4,1)|UNIFORM BEHAVIOR(4,1)|UNITED NATIONS ENVIRONMENT(4,1)|UPWARD DRIFT(4,1)|INJECTION PUMP(3,4)|ALKALINITY(3,1)|AMPHIBOLITE(3,1)|ANNULUS SPACE(3,1)|AQUEOUS ACIDIC SOLUTION(3,1)|ATMOSPHERIC CARBON DIOXIDE CONVERSION(3,1)|AVIATION(3,1)|BASALT(3,1)|BIOMASS(3,1)|BOREHOLE WATER(3,1)|CA2MG5SI8O(3,1)|CAMGSI2O(3,1)|CAMGSIO(3,1)|CARBON CAPTURE MODULE(3,1)|CARBON CAPTURE PLANT(3,1)|CARBON DIOXIDE INJECTION MODULE(3,1)|CO2 ABATEMENT DEGREE(3,1)|CO2 EMITTING INDUSTRIAL PLANT(3,1)|CO2 FIXATION(3,1)|CO2 LOSS(3,1)|CO2 SATURATED FLUID(3,1)|CO2 STORAGE TANK(3,1)|CONFIRMATION(3,1)|CREVICE(3,1)|DAYTIME(3,1)|DOSING RATE(3,1)|DROUGHT(3,1)|DUNITE(3,1)|ELECTRICAL STORAGE FACILITY(3,1)||(US20230038447)|CARBON DIOXIDE(100,41)|CARBON DIOXIDE SEQUESTRATION(100,13)|RENEWABLE ENERGY SOURCE(100,11)|IN SITU MINERALIZATION(100,2)|PERIDOTITE IN SITU MINERALIZATION(100,1)|PACKER MODULE(76,3)|ROCK FORMATION(74,16)|PERIDOTITE ROCK(67,6)|INJECTION TUBING(52,1)|SYNCHRONIZED BIOFUEL GENERATOR(52,1)|GAS DISSOLUTION MODULE(48,9)|MINIMAL INTERRUPTION(47,1)|PERFORATION(45,11)|MIXTURE EJECTION(45,1)|BIO FUEL GENERATOR(42,4)|CO2 RICH INJECTION(40,4)|FINANCIAL TERM(37,1)|NATURAL WEATHERING(37,1)|SOLAR INVERTER(37,1)|CO2 RICH(36,22)|EVAPORATIVE COOLING(36,2)|INJECTION INTERVAL HYDRAULIC ISOLATION(35,1)|SUBSURFACE MODULE(35,1)|MAGNESITE(34,4)|RECYCLING WATER(34,1)|PERIDOTITE(33,16)|SOLAR PHOTOVOLTAIC PANEL(33,1)|PERMEABLE ZONE(32,1)|SERVICING(32,1)|MINERALIZATION REACTION(31,2)|CALCITE(30,4)|CARBONATE ROCK(30,2)|GAS DISSOLUTION(30,1)|BUBBLE DIAMETER(29,1)|INFLATE AQUEOUS SOLUTION(29,1)|CO2(27,41)|BIO FUEL ENERGY(27,1)|LIVE MONITORING(26,2)|HYBRID RENEWABLE(25,2)|REACTION PATHWAY(23,6)|MINIMUM LM(23,1)|DOWNSTREAM PRESSURE(22,1)|IDENTIFIED DEPTH(22,1)|INTERNAL ACCESS(22,1)|LENGTH PERFORATION(21,1)|PROJECT APPLICATION ACCOUNTING(21,1)|SOLAR ENERGY MODULE(21,1)|INJECTION WELL TUBING(20,5)|CARBON FOOTPRINT(19,1)|HYDROELECTRICITY(19,1)|NONCORROSIVE INJECTION WELL TUBING(19,1)|RETURN FLUID(18,9)|NONCORROSIVE WELL CASING(17,1)|RECYCLING WATER RECYCLED BACK(16,1)|PERIDOTITE VOLUME(15,7)|MGCO3(15,2)|CO2 DISSOLUTION(14,7)|CACO3(14,2)|FLUID VOLUME(14,1)|GEOTHERMAL ENERGY(14,1)|NONCORROSIVE WELL INJECTION TUBING(14,1)|SLOW FLOW VELOCITY(14,1)|WIRING(14,1)|MONITORING BOREHOLE(13,4)|OBSERVATION WELL(13,4)|HYDROSTATIC PRESSURE SENSOR(13,1)|WIND TURBINE(12,3)|INJECTION POINT(12,2)|PERIDOTITE RESERVOIR(12,2)|ARTIFICIAL CONSERVATIVE TRACER(12,1)|CARBON FOOTPRINT LOW(12,1)|DISSOLUTION RESIDENCE TIME(12,1)|GAS FLOW(12,1)|HYDRO ENERGY(12,1)|MINERALIZATION TIME(12,1)|MINIMUM TEMPERATURE(12,1)|SURFACE PACKER CONTROLLER(12,1)|INJECTION WELL(11,18)|HYBRID ENERGY SOURCE(11,1)|INJECTED CONSERVATIVE TRACER(11,1)|INJECTION BOREHOLE DEEP PERFORATION(11,1)|INJECTION BOREHOLE PERFORATION(11,1)|MAGNESIA PERIDOTITE ORE PRODUCTION(11,1)|NATURAL PERIDOTITE CARBONATION(11,1)|NONCORROSIVE CASING PERMANENT INSTALLATION(11,1)|OLIVINE CARBONATION(11,1)|PERFORATION CAREFUL PLACEMENT(11,1)|PERIDOTITE MINERALIZATION(11,1)|PERIDOTITE NATURAL CARBONATION(11,1)|PERIDOTITE REACTIVITY(11,1)|POLLUTANT REMEDIATION(11,1)|PYROXENE MINERAL LESSER PROPORTION(11,1)|RENEWABLE ENERGY STORAGE MODULE(10,2)|SUBMERSIBLE PUMP(9,13)|PACKED OFF INTERVAL(9,4)|TARGET INJECTION ZONE(9,4)|AMBIENT RESERVOIR GROUNDWATER(9,1)|DATA ACQUISITION(9,1)|FLOWING MIXTURE(9,1)|GREEN ENERGY SOURCE(9,1)|PERIDOTITE IGNEOUS ROCK(9,1)|RECOVERY BOREHOLE COLLECT(9,1)|SWITCH GEAR(9,1)|TECTONICALLY EXPOSED PERIDOTITE(9,1)|WIND ENERGY(9,1)|WELL CASING(8,6)|PACKER TOOL(8,2)|CO2 EFFERVESCENCE(8,1)|CO2 LATE INJECTION(8,1)|CO2 MINERALIZATION CAPACITY(8,1)|DEEP BOREHOLE(8,1)|DOWNHOLE INJECTION PIPING(8,1)|FIXATION CO2 ABSORPTION(8,1)|GLACIER RETREAT(8,1)|H2S ABATEMENT(8,1)|INJECTED CO2 RICH MONITORING(8,1)|INOSILICATE MINERAL(8,1)|MANTLE PERIDOTITE(8,1)|OBSERVED CLIMATE CHANGEOVER(8,1)|PERIDOTITE TARGET ZONE(8,1)|POLLUTANT SUPPRESSION(8,1)|RECONNAISSANCE MAPPING(8,1)|RECOVERING BOREHOLE(8,1)|RETURN FLUID WELL(8,1)|SENSITIVE THERMODYNAMIC BEHAVIOR(8,1)|SERPENTINE REACTANT(8,1)|STANDBY WING(8,1)|SUBMERSIBLE INTAKE PUMP(8,1)|SUBSURFACE CONNECTIVITY(8,1)|CO2 MOLAR RATIO(7,3)|CO2 TANK(7,2)|GAS FLOW RATE(7,2)|OLIVINE REACTION(7,2)|PERIDOTITE LAYER(7,2)|TRACER FLUID(7,2)|ABUNDANT MINERAL(7,1)|ANTHROPOGENIC IMPACT(7,1)|BUFFER TANK SIZING(7,1)|BULK ROCK FRACTURE STRESS(7,1)|CO2 COLLISION(7,1)|CO2 FIXATION DECREASE(7,1)|CO2 RICH RELEASE(7,1)|DARCY LAW(7,1)|DISSOLVED CO2 SOLUBILITY(7,1)|DOWNSTREAM END(7,1)|EARTH MANTLE(7,1)|FLUID RESIDENCE TIME(7,1)|GAS INFLATION PACKER(7,1)|GEOLOGICAL RESERVOIR(7,1)|GLOBAL WARMING SUPPRESSION(7,1)|HYDROUS ALTERATION PRODUCT(7,1)|INJECTION BOREHOLE WALL(7,1)|LIQUID CONSERVATIVE TRACER(7,1)|MAGNESIA PURITY(7,1)|MG CARBONATION(7,1)|MINERAL OLIVINE(7,1)|NONCORROSIVE PIPE(7,1)|OBSERVATION BOREHOLE FLUID(7,1)|OUTGOING SAMPLING PORT(7,1)|PERFORATION DEPTH(7,1)|PERIDOTITE PERMEABLE LAYER(7,1)|PERIDOTITE ROCK FORMATION(7,1)|POLYMER TUBING STRING(7,1)|PROGRAM REPORT(7,1)|RECOVERY BOREHOLE DEPTH(7,1)|SOLUBILIZED CO2(7,1)|UNINTERRUPTED CO2(7,1)|UNINTERRUPTED DRAW(7,1)|UPSTREAM END(7,1)|POROSITY(6,4)|FLUID INJECTION(6,3)|ACCURATE ACCOUNTING(6,1)|BIO FUEL MODULE(6,1)|BOREHOLE FULL DEPTH(6,1)|BURNING FOSSIL FUEL(6,1)|CARBONATION REACTION(6,1)|CO2 EMISSION(6,1)|DILUTION CALCULATION(6,1)|DISSOLVED CO2 ANALYSIS(6,1)|DOMINANT INFLUENCE(6,1)|INJECTION PIPELINE(6,1)|INJECTION PORTABILITY(6,1)|MAXIMIZE BUBBLE(6,1)|MONITORING OBSERVATION BOREHOLE(6,1)|NATURAL FRACTURE NETWORK(6,1)|NATURAL TRACER(6,1)|PAST CENTURY(6,1)|PAST DECADE(6,1)|PERIDOTITE GEOLOGIC FORMATION(6,1)|PERMANENTLY SEQUESTERING CARBON DIOXIDE(6,1)|SEA FLOOR(6,1)|STABLE CARBONATE MINERAL(6,1)|SUBTERRANEAN GEOLOGIC FORMATION(6,1)|TARGET SETPOINT(6,1)|TRACER MOLAR RATIO(6,1)|TRACER SUBSTANCE(6,1)|UNDISSOLVED CO2 GAS BUBBLE(6,1)|PHOTOVOLTAIC(5,3)|ATMOSPHERIC CO2(5,2)|FINE POWDER(5,2)|H2S GAS BUBBLE(5,2)|INTERMITTENCY(5,2)|LOW PRESSURE ZONE(5,2)|MG3SI2O(5,2)|PRETREATMENT(5,2)|REAGENT(5,2)|SEAWATER(5,2)|TARGET FORMATION(5,2)|BOOSTER PUMP(4,4)|DOSING PUMP(4,4)|MBGL(4,4)|AQUEOUS SOLUTION(4,3)|CARBONIC ACID(4,3)|PRESSURIZED WATER STREAM(4,3)|RETURN FLUID PIPE(4,3)|DRILLING(4,2)|ABSORPTION ENHANCEMENT(4,1)|ACCELERATE REMOVAL(4,1)|ALTERATION NATURE(4,1)|ARTIFICIALLY PRODUCED CA(4,1)|ATMOSPHERIC CARBON DIOXIDE YEAR(4,1)|BOREHOLE SINGLE HEMISPHERE(4,1)|BUOYANCY(4,1)|CHEMICAL WEATHERING ACCELERATION(4,1)|CO2 EMITTING INDUSTRY(4,1)|CO2 PERIDOTITE REACTION(4,1)|CO2 PYROXENE REACTION(4,1)|CO2 STORAGE FACILITY(4,1)|CONTROL PANEL(4,1)|DAMPENING PRESSURE FLUCTUATION(4,1)|FLUID FLOWPATH(4,1)|FOSSIL FUEL CONSUMPTION(4,1)|FUZED PHOSPHATE(4,1)|GEOLOGICAL FORMATION TARGET ZONE(4,1)|HEAD UNIT(4,1)|HOMOGENEOUS NATURE(4,1)|HYBRID CONTROLLER(4,1)|HYDRAULIC COMMUNICATION(4,1)|INCOMING INJECTION FLUID(4,1)|INJECTED FLUID HOMOGENOUS NATURE(4,1)|INJECTION ZONE INTERVAL(4,1)|INSTRUMENTALITY(4,1)|INTERMITTENT NATURE(4,1)|ISOLATED INJECTION INTERVAL(4,1)|LIMITING NATURAL FRACTURE(4,1)|MAGNESIUM SINKING PROCESSING(4,1)|MAGNETIC BEHAVIOR(4,1)|MONITORING MODULE(4,1)|NIGHT LOAD(4,1)|NONCORROSIVE FLUID PIPE(4,1)|OVERPRESSURE(4,1)|PERIDOTITE FORMATION ILLUSTRATION(4,1)|PERIDOTITE MAGNESIUM OXIDE(4,1)|PERIDOTITE MAXIMUM DEPTH(4,1)|PERMEABILITY TEST(4,1)|PLACEMENT DEPTH(4,1)|PRIMARY WING(4,1)|PROPRIETY(4,1)|REMOVING IMPURITY(4,1)|RETURN BOREHOLE WALL(4,1)|SIZE WELL INJECTION TUBING(4,1)|SOLID CARBONATE MINERAL(4,1)|SUBSURFACE FORMATION(4,1)|TARGET INJECTION INTERVAL(4,1)|TREATING CO2(4,1)|UNDERGROUND ROCK FORMATION(4,1)|UNIFORM BEHAVIOR(4,1)|UNITED NATIONS ENVIRONMENT(4,1)|UPWARD DRIFT(4,1)|INJECTION PUMP(3,4)|ALKALINITY(3,1)|AMPHIBOLITE(3,1)|ANNULUS SPACE(3,1)|AQUEOUS ACIDIC SOLUTION(3,1)|ATMOSPHERIC CARBON DIOXIDE CONVERSION(3,1)|AVIATION(3,1)|BASALT(3,1)|BIOMASS(3,1)|BLOCKAGE(3,1)|BOREHOLE WATER(3,1)|CAMGSI2O(3,1)|CARBON CAPTURE MODULE(3,1)|CARBON CAPTURE PLANT(3,1)|CARBON DIOXIDE INJECTION MODULE(3,1)|CO2 ABATEMENT DEGREE(3,1)|CO2 EMITTING INDUSTRIAL PLANT(3,1)|CO2 FIXATION(3,1)|CO2 LOSS(3,1)|CO2 SATURATED FLUID(3,1)|CO2 STORAGE TANK(3,1)|CONFIRMATION(3,1)||(JP7384477)|CARBON DIOXIDE(100,66)|INJECTION WELL(100,47)|RENEWABLE ENERGY SOURCE(100,29)|ROCK LAYER(100,29)|CARBON DIOXIDE ISOLATION(100,14)|GAS(100,14)|GAS DISSOLUTION MODULE(100,14)|WELL CASING(100,13)|PACKER MODULE(100,10)|CARBON DIOXIDE MIXED LIQUID(100,9)|MIXED LIQUID(100,9)|IN SITU MINERALIZATION(100,6)|CARBON DIOXIDE SEQUESTRATION(100,3)|CONTROLLED STRENGTHENING(100,3)|HYBRID ENERGY SOURCE(100,3)|NONCORROSIVE INJECTION WELL(100,3)|NONCORROSIVE WELL CASING(100,3)|PERIDOTITE IN SITU MINERALIZATION(100,3)|DISCHARGE PORT(100,2)|SEAL LENGTH(100,2)|BIO FUEL GENERATOR(59,7)|RHOMBIC EARTH(58,2)|CO2 MINERALIZATION(52,4)|NATURALLY OCCURRING PERIDOTITE(52,1)|ABOVEGROUND MODULE(50,1)|SYNCHRONOUS BIOFUEL GENERATOR(49,3)|SILICATE MINERAL WEATHERING RATE(49,1)|PERIDOTITE(47,39)|LIVE MONITORING(45,3)|ACCELERATE REMOVAL(44,1)|CARBONATE MINERAL(42,2)|CARBONATE CHLORIDE(41,3)|SERPENTINE REACTION PRODUCT(38,1)|WEATHERING RATE(38,1)|PERFORATION(35,14)|SOLAR INVERTER(35,4)|CARBON CAPTURE PLANT(35,1)|UPSTREAM TEMPERATURE(34,1)|ACCELERATION(31,1)|REQUIRING PROCESSING(31,1)|PERIDOTITE ROCK LAYER(30,4)|SOLAR ENERGY MODULE(30,3)|FINE POWDER(30,2)|DOWNSTREAM TEMPERATURE(28,1)|CO2(27,52)|OBSERVATION BOREHOLE(26,8)|CALCITE(26,4)|OLIVINE(26,2)|CARBON STORAGE(26,1)|BIO FUEL ENERGY(25,3)|CARBON DIOXIDE REACTION(24,2)|ECONOMIC LIGHT RAY(23,1)|RECIRCULATING(22,2)|TRANSMISSION ZONE(22,2)|SILICATE MINERAL(21,3)|WIRING(21,3)|CO2 DISSOLUTION(20,8)|WIND TURBINE(20,5)|RECIRCULATION(20,4)|HYDROSTATIC PRESSURE SENSOR(20,3)|FED WELL PIPING(19,1)|RENEWABLE ENERGY STORAGE MODULE(18,3)|OBSERVATION WELL(17,13)|PERIDOTITE LAYER(17,9)|CARBON DIOXIDE SOURCE(17,1)|ENERGY CONSUMPTION(17,1)|PERIDOTITE SITU CARBONATION(17,1)|RENEWABLE ENERGY(16,5)|UNDERGROUND STRATA PERMEABILITY(16,1)|MONITORING BOREHOLE(15,4)|SUBMERGED PUMP(14,4)|FLUID VOLUME(14,3)|INJECTION POINT(14,2)|PERIDOTITE RESERVOIR(14,2)|SOLAR PANEL(14,2)|ARTIFICIAL CONSERVATIVE TRACER(14,1)|CO2 FIXATION(13,3)|DATA ACQUISITION(13,3)|GEOTHERMAL ENERGY(13,3)|PUMPING SECTION(13,3)|DISSOLVED INORGANIC CARBON(13,1)|FED WELL(13,1)|FERMENTALITE WEATHERING(13,1)|INJECTED CONSERVATIVE TRACER(13,1)|INJECTION BOREHOLE DEEP PERFORATION(13,1)|MOLTEN PHOSPHORUS MANURE(13,1)|PERIDOTITE MINERALIZATION(13,1)|PERIDOTITE REACTIVITY(13,1)|REFORMING INDUSTRIAL POLLUTANT(13,1)|TOO SLOW(13,1)|UNDISSOLVED CO2 BUBBLE(13,1)|PUMP HEAD(12,4)|ADMINISTRATION PUMP(12,3)|BOREHOLE OBSERVATION(12,3)|INJECTION HEAD UNIT(12,3)|MINIMUM TEMPERATURE(12,3)|MINERAL PERIDOTITE(12,2)|NONCORROSIVE PIPE(12,2)|PYROXENE(11,7)|REACTION RATE(11,5)|TARGET INJECTION ZONE(11,4)|DOWNSTREAM END(11,3)|HYDRAULIC POWER(11,3)|RENEWABLE ENERGY STORAGE(11,3)|UPSTREAM END(11,3)|UNDERGROUND MODULE(11,2)|BELOW GROUND MODULE(11,1)|DIAMETRICAL ROCK(11,1)|DOWNHOLE INJECTION PIPING(11,1)|PERIDOLITE DISSOLUTION(11,1)|PERIDOTITE IGNEOUS ROCK(11,1)|PERIDOTITE MAGNESIA(11,1)|RECOVERY BOREHOLE COLLECT(11,1)|UNFIRED PERIDOTITE(11,1)|CO2 MOLAR RATIO(10,3)|PACKER TOOL(10,2)|UNDERWATER PUMP(10,2)|BOROSILICATE MINERAL(10,1)|BRIGHT MINERAL PROPORTION(10,1)|CARBONATE VEIN YEAR(10,1)|CO2 MINERALIZATION CAPACITY(10,1)|DRILLING PENETRANCE(10,1)|ELECTROMAGNETIC FLOWMETER(10,1)|ENHANCE MAGNESIA PURITY(10,1)|FLOATATION DRESSING(10,1)|MANTLE PERIDOTITE(10,1)|NONCORROSIVE CASING(10,1)|NONLIMITED FUEL PANEL(10,1)|RECOVERED BOREHOLE DEPTH(10,1)|RELEASING CO2 BUBBLE(10,1)|RETURN FLUID WELL(10,1)|SENSITIVE THERMODYNAMIC BEHAVIOR(10,1)|STRATUM TARGET ZONE(10,1)|SUBSURFACE ROCK(10,1)|ULTRAMETRICAL ROCK(10,1)|UNDERWATER INTAKE PUMP(10,1)|SUBMERSIBLE PUMP(9,9)|PRESSURE SENSOR(9,3)|NATURAL CRUSH(9,2)|PERIDOTITE FORMATION(9,2)|POROSITY(8,4)|GREEN ENERGY SOURCE(8,3)|HYDRAULIC ENERGY(8,3)|WIND ENERGY(8,3)|ABSORPTION CONFIRMATION(8,1)|ABUNDANT MINERAL(8,1)|BAKED SHELL POWDER(8,1)|BULK ROCK FRACTURE STRESS(8,1)|BURNING FOREST(8,1)|CO2 EMITTING INDUSTRY(8,1)|CO2 SECURE SOLUBILITY(8,1)|EARTH MANTLE(8,1)|GLOBAL WARMING PREVENTION(8,1)|H2S BUBBLE(8,1)|INJECTION BOREHOLE WALL(8,1)|INJECTION PORTABILITY(8,1)|INJECTION REARRANGEMENT(8,1)|MINERALIZATION GENERATION(8,1)|MINERALIZATION SITE(8,1)|OUTFLOW SAMPLING PORT(8,1)|PERFORATION DEPTH(8,1)|PERIDOLITE CARBONIC CHLORIDE(8,1)|PYROXITE MINERAL(8,1)|RHOMBIC ROCK(8,1)|ROCK PERMEABILITY(8,1)|SOLUBILIZED CO2(8,1)|STANDBY BLADE(8,1)|TRACER SUBSTANCE(8,1)|TRANSMISSIBLE ZONE(8,1)|UNDERGROUND DILUTION(8,1)|UNINTERRUPTED SUCTION(8,1)|DISCLOSURE SUBJECT(7,7)|HEMISPHERE(7,3)|STRING(7,3)|GROUNDWATER(7,2)|ATMOSPHERIC CO2 CONCENTRATION TREND(7,1)|BIO FUEL MODULE(7,1)|CAPTURED CO2(7,1)|CARBONATE ROCK(7,1)|CARBONATION REACTION(7,1)|CO2 EMISSION(7,1)|CRUSH NETWORK(7,1)|DISSOLVED CO2 ANALYSIS(7,1)|DOMINANT IMPACT(7,1)|EXTRUSION ZONE(7,1)|FIXING CO2 DECREASE(7,1)|FOSSIL FUEL COMBUSTION(7,1)|INJECTED CO2(7,1)|INJECTION PIPELINE(7,1)|INORGANIC REACTION ACCELERATOR(7,1)|MAGNESIUM PRECIPITATION TREATMENT(7,1)|MINERALIZATION REACTION(7,1)|MINIMAL DISRUPTION(7,1)|NATURAL TRACER(7,1)|NUCLEOTIDE HALOGENATED SUBSTANCE(7,1)|OLIVINE RESERVOIR LAYER(7,1)|PAST CENTURY(7,1)|PAST FEW DECADE(7,1)|PERFORATION CAREFUL ARRANGEMENT(7,1)|PERIDOLITE REACTION(7,1)|PERIDOTITE MAXIMUM DEPTH(7,1)|PILOT SCALE EXPERIMENT(7,1)|POLLUTANT TREATMENT(7,1)|SLOW PERMEABILITY(7,1)|TRACER MOLAR RATIO(7,1)|TRACER TANK(7,1)|UNINTERRUPTED CO2 SUPPLY(7,1)|WATER INFLATION PACKER(7,1)|CONTROL PANEL(6,3)|INJECTION WELL PIPING(6,3)|ALKALINITY(6,2)|CO2 SATURATED FLUID(6,2)|CONTAMINANT(6,2)|FLUID COMMUNICATION(6,2)|RECIRCULATED WATER(6,2)|SEAWATER(6,2)|BOOSTER PUMP(5,4)|CRACK(5,4)|GROUND STORAGE TANK(5,4)|REACTION PATH(5,4)|CARBONIC ACID(5,3)|GEOLOGICAL LAYER(5,3)|GROUND PACKER CONTROL DEVICE(5,3)|MANGANESE(5,3)|RETURN FLUID PIPE(5,3)|CLOG(5,2)|GAS DISSOLUTION(5,2)|ALLEVIATING PRESSURE FLUCTUATION(5,1)|ARTIFICIALLY PRODUCED CA(5,1)|CO2 ADDITION(5,1)|CO2 AIR BUBBLE COLLISION(5,1)|CO2 LOSS(5,1)|CO2 OLIVINE REACTION(5,1)|CO2 STORAGE FACILITY(5,1)|COMPRESSED CO2(5,1)|DISSOLVED CO2 CONTENT(5,1)|DRILLED HOLE(5,1)|ELECTRICITY GENERATION(5,1)|EVAPORATION COOLING(5,1)|EXPAND AQUEOUS SOLUTION(5,1)|GAS DISSOLVING MODULE(5,1)|GEOLOGICAL STRATA(5,1)|GEOLOGICAL SUBSTANCE PLACE(5,1)|GEOLOGICAL TIMESCALE(5,1)|HYBRID CONTROLLER(5,1)|INFLOW FLUID(5,1)|INSTALLATION DEPTH(5,1)|LATE INJECTION(5,1)|MONITORING MODULE(5,1)|NIGHT LOAD(5,1)|NONCORROSIVE FLUID PIPE(5,1)|OBSERVED BOREHOLE FLUID(5,1)|PERIDOTITE TRANSMISSION LAYER(5,1)|PERMEABILITY TEST(5,1)|REMOVING IMPURITY(5,1)|RENEWABLE ENERGY SURPLUS(5,1)|REPORTING PROGRAM(5,1)|RETURN BOREHOLE WALL(5,1)|SHORT BOREHOLE(5,1)|SITE CONSUMPTION(5,1)|SOLID CARBONATE MINERAL(5,1)|SUPPLYING CO2(5,1)|TESTING CATION(5,1)|TOTAL MINERALIZATION(5,1)|TRACER FLUID(5,1)|TREATING CO2(5,1)|UNITED NATIONS ENVIRONMENT(5,1)|ACIDIC AQUEOUS SOLUTION(4,1)|AGRICULTURE(4,1)|ATMOSPHERIC CARBON DIOXIDE(4,1)|AVIATION(4,1)|BASALT(4,1)|BIOFUEL(4,1)|BIOMASS(4,1)|BIOPANEL(4,1)|BUOYANCY(4,1)|CARBON CAPTURE MODULE(4,1)|CARBON DIOXIDE INJECTION MODULE(4,1)|CO2 IMMOBILIZATION(4,1)|CO2 RICH FLUID(4,1)|CO2 TANK PRESSURE(4,1)|CONNECTOR COUPLING(4,1)|DANITE(4,1)|DISSOLUTION RATE(4,1)|DROUGHT(4,1)|ELECTRICITY STORAGE FACILITY(4,1)|EXCAVATION(4,1)|FIXED CO2 ABSORPTION(4,1)|FLANGED PIPE SECTION(4,1)|FLUID INJECTION(4,1)|GAS LEAKAGE(4,1)|GEOLOGICAL STORAGE LAYER(4,1)|GLACIATION(4,1)|HORNITE(4,1)|HUMAN INFLUENCE(4,1)|HURRICANE(4,1)|IMPURITY ACID LEACHING REMOVAL(4,1)|INFUSION RATE(4,1)|INJECTION BOREHOLE INJECTION SECTION(4,1)|INJECTION COLUMN(4,1)|INJECTION FLUID(4,1)|INJECTION LIQUID(4,1)|INJECTION PIPE COLUMN(4,1)||(JP2023024948)|CARBON DIOXIDE(100,49)|RENEWABLE ENERGY SOURCE(100,21)|IN SITU MINERALIZATION(100,4)|OLIVINE IN SITU MINERALIZATION(100,2)|CARBON DIOXIDE SEQUESTRATION(100,1)|CO2 INSITU MINERALIZATION(100,1)|OLIVINE SERUM(65,1)|ROCK BED(60,8)|PACKER MODULE(56,6)|PERIDOTITE FORMATION(54,2)|CARBON DIOXIDE ISOLATION(53,9)|SYNCHRONOUS BIOFUEL GENERATOR(51,2)|NATURALLY OCCURRING OLIVINE(48,1)|NATURAL WEATHERING(47,1)|NONCORROSIVE(47,1)|GAS DISSOLUTION MODULE(45,14)|BIO FUEL GENERATOR(45,6)|GRIND MODULE(42,2)|INGRESS LOCATION(40,1)|MIXTURE DISCHARGE(40,1)|OLIVINE(39,26)|PERMEATION ZONE(38,1)|RHOMBUS(38,1)|MINERALIZATION REACTION(36,2)|CARBONATE ROCK(35,2)|CO2SYSTEMS(35,1)|SOLAR INVERTER(34,3)|UNDERGROUND MODULE(34,2)|AGRICULTURE(34,1)|CARBON CAPTURE PLANT(34,1)|PERFORATION(33,13)|CALCITE(33,5)|CRACK(32,3)|GROUND PACKER CONTROLLER(32,2)|UPSTREAM TEMPERATURE(32,1)|ROCK LAYER(31,17)|RECYCLING WATER(31,2)|AVIATION(31,1)|CO2(31,1)|CARBONATION(30,2)|CEMENT CONCRETE(30,1)|MIXED SOLUTION(30,1)|LIVE MONITORING(28,3)|BOREHOLE(27,19)|MINERALIZATION(27,4)|REACTION PATHWAY(27,4)|DOWNSTREAM TEMPERATURE(27,1)|MAGNOLITE(27,1)|BIO FUEL ENERGY(26,2)|CARBON STORAGE(25,1)|CARBON DIOXIDE MIXED SOLUTION(24,1)|COLLECTION BOREHOLE(22,7)|PETROLEUM(22,2)|NATURALLY OCCURRING(21,1)|OPENER(21,1)|TUBING(20,3)|INJECTION LINE(20,1)|CO2CO(19,4)|RECIRCULATION(19,3)|COAL(19,2)|SOLAR ENERGY MODULE(19,2)|MGCO3(18,2)|OLIVINE ROCK MINERALIZATION(18,1)|INJECTION WELL(17,19)|OBSERVATION BOREHOLE(17,4)|RECOVERY BOREHOLE(17,4)|PHOTOVOLTAIC POWER PANEL(17,2)|OMAN MANTLE OLIVINE(17,1)|PERIDOTITE SITU CARBONATION(17,1)|RECIRCULATING WATER BACK(17,1)|WELL INJECTION PIPING(16,3)|STORAGE OPERATION(16,2)|BOREHOLE OBSERVATION(15,5)|RENEWABLE ENERGY(15,5)|MONITORING BOREHOLE(15,4)|FLUID VOLUME(15,2)|NONCORROSIVE WELL CASING(15,2)|CARBON DIOXIDE SOURCE(15,1)|MAGNESIA OLIVINE ORE(15,1)|RECOVERY RATE(15,1)|WELL OBSERVATION(14,4)|WIND TURBINE(14,4)|CONSERVATIVE TRACER(14,2)|GEOTHERMAL ENERGY(14,2)|POURED WELL(14,2)|WIRING(14,2)|MINERALIZATION TIME(14,1)|SUBTERRANEAN FORMATION PREMECHANICAL CRUSHING(14,1)|RENEWABLE ENERGY STORAGE MODULE(13,2)|EXPRESSION SECTION(12,5)|GLOBAL CLIMATE FLUCTUATION(12,2)|GLOBAL WARMING SUPPRESSION(12,2)|MINIMUM TEMPERATURE(12,2)|NONCORROSIVE PIPE(12,2)|OLIVINE RESERVOIR(12,2)|DISSOLVED CO2AN UNDERWATER PUMP(12,1)|INJECTION BOREHOLE CO2IS(12,1)|INJECTION BOREHOLE INJECTION WELLHEAD(12,1)|OLIVINE CARBONATION(12,1)|OLIVINE MINERALIZATION(12,1)|OLIVINE NATURAL CARBONATION(12,1)|PERFORATION CAREFUL PLACEMENT(12,1)|TARGET INJECTION ZONE(11,4)|CO2ACTIVATE OLIVINE FORMATION(11,1)|EVAPORATIVE CHILLER(11,1)|FLOWING MIXTURE(11,1)|FOSSIL FUEL CO2THE EMISSION(11,1)|GEOLOGICALLY EXPOSED OLIVINE(11,1)|GLITTER MINERAL PROPORTION(11,1)|INJECTION BOREHOLE WELLHEAD(11,1)|OBSERVED BOREHOLE 2IT(11,1)|OLIVINE CO2THE COLUMN(11,1)|RICH FLUID MIXTURE2THE FIXATION(11,1)|SOLUBLE PHOSPHORUS FERTILIZER(11,1)|SUBTERRANEAN FORMATION CO2BENEFITS(11,1)|SUBTERRANEAN FORMATION2IS(11,1)|UNCALCINED OLICORITE(11,1)|CASTING WELL(10,4)|ELECTRICAL POWER(10,2)|HYBRID ENERGY SOURCE(10,2)|PACKER TOOL(10,2)|SEAL LENGTH(10,2)|BOREHOLE CO2TO(10,1)|CLIMATIC FLUCTUATION(10,1)|CO2CONSIDERABLE EFFORT(10,1)|CO2THE PACKER(10,1)|DEEP BOREHOLE(10,1)|INJECTED CO2UNDERWATER PUMP(10,1)|INJECTION BOREHOLE CO2THE DECREASE(10,1)|INOSILICATE MINERAL(10,1)|INVESTIGATIONAL MAPPING(10,1)|NATIONAL ENVIRONMENTAL PLANNING REPORT(10,1)|NONCORROSIVE CASING(10,1)|OLIVINE CO2MOLAR RATIO(10,1)|OLIVINE CO2THE REACTION(10,1)|OLIVINE DISSOLUTION(10,1)|OLIVINE SUBTERRANEAN FORMATION(10,1)|OLIVINE TARGET ZONE(10,1)|PRIMARILY MINERAL OLIVINE(10,1)|RHOMBIC BITTER(10,1)|SENSITIVE THERMODYNAMIC BEHAVIOR(10,1)|SUPERBITTER STONE(10,1)|TRACER CO2THE(10,1)|UNDERWATER INTAKE PUMP(10,1)|UNINTERRUPTED ASPIRATION(10,1)|NATURAL FRACTURE(9,3)|OLIVINE VOLUME(9,3)|DATA ACQUISITION(9,2)|GREEN ENERGY SOURCE(9,2)|UPSTREAM END(9,2)|WIND ENERGY(9,2)|POROSITY(8,4)|PUMP HEAD(8,3)|STORED ENERGY(8,3)|INJECTION HEAD UNIT(8,2)|OLIVINE ROCK LAYER(8,2)|SUBMERGED PUMP(8,2)|TRACER FLUID(8,2)|ABUNDANT MINERAL(8,1)|ARTIFICIALLY MANUFACTURED CA(8,1)|ATMOSPHERIC CO2THIS(8,1)|ATMOSPHERIC CO2WAS(8,1)|BIO FUEL MODULE(8,1)|BULK ROCK BREAKING STRESS(8,1)|BURNING FOREST(8,1)|CO2A NONCORROSIVE FLUID PIPE(8,1)|CO2A PERMEABILITY TEST(8,1)|CO2MINERALIZATION CAPABILITY(8,1)|CO2THE DISPERSION(8,1)|COLLECTED BOREHOLE DEPTH(8,1)|DARCY LAW(8,1)|DELIVER DAILY REQUIREMENT(8,1)|DELIVER NIGHTTIME LOAD(8,1)|DISSOLVED CO2AN ANALYSIS(8,1)|DOWNHOLE FIRING(8,1)|DRILLING PENETRATION(8,1)|ECONOMIC STANDPOINT(8,1)|FLOTATION PURIFICATION(8,1)|GAS INFLATION PACKER(8,1)|GROUND CO2TAKING(8,1)|H2O H2CO3H(8,1)|H2O MG3SI2O(8,1)|HYDROUS VARIANT(8,1)|INJECTED BOREHOLE WALL(8,1)|INJECTED CO2CAN(8,1)|INJECTED CO2THE(8,1)|INJECTION BOREHOLE DEVELOPMENT(8,1)|LIQUID PRESERVATION TRACER(8,1)|MAGNESIA PURITY(8,1)|MAGNESIA RECOVERY(8,1)|MG CARBONATION(8,1)|MINERALIZATION SITE(8,1)|OLIVINE BURN(8,1)|OUTFLOW SAMPLING PORT(8,1)|POLYMER TUBING STRING(8,1)|PUMPING INTERRUPTION(8,1)|RADISTONE MINERAL(8,1)|ROCK PERMEABILITY(8,1)|STANDBY BLADE(8,1)|STANDBY CO2ENSURE SUPPLY(8,1)|SUBTERRANEAN DILUTION(8,1)|SUBTERRANEAN ROCK FORMATION(8,1)|TARGET ZONE UNCASING(8,1)|VIEWING BOREHOLE(8,1)|WATER CO2AND H2THE PH(8,1)|OBSERVATION WELL(7,7)|CO2IT(7,2)|DOWNSTREAM END(7,2)|INJECTION WELL PIPING(7,2)|ABSORPTION ACCELERATOR(7,1)|BIO FUEL DRIVEN GENERATOR(7,1)|CARBONATE AVERAGE YEAR(7,1)|CARBONATION REACTION(7,1)|CO2A GAS DISSOLUTION MODULE(7,1)|CO2IS MOLAR RATIO(7,1)|CO2RICH FLUID(7,1)|CO2SATURATED FLUID(7,1)|COMPRESSED CO2MAY(7,1)|DRILLING DEPTH(7,1)|EARTH MANTLE(7,1)|FORMULA CO2WITH(7,1)|FRACTURE NETWORK(7,1)|GEOLOGICAL SUBSTANCE LOCATION(7,1)|GROUND INJECTION WELLHEAD(7,1)|HARMFUL SUBSTANCE(7,1)|INJECTION PIPELINE(7,1)|INJECTION PORTABILITY(7,1)|LATE INJECTING(7,1)|LIGHT CALCINED DOLOMITE(7,1)|MAGNESIUM PRECIPITATION TREATMENT(7,1)|MINIMAL INTERRUPTION(7,1)|NATURAL FLUCTUATION(7,1)|NATURAL TRACER(7,1)|PAST DECADE(7,1)|PERMEABLE ZONE(7,1)|PILOT SCALE EXPERIMENT(7,1)|SHUTDOWN TOOL(7,1)|SIO4AND MG(7,1)|SOLAR MODULE(7,1)|SUBTERRANEAN FORMATION TARGET ZONE(7,1)|TRACER MOLAR RATIO(7,1)|TRACER TANK(7,1)|TREATING CONTAMINANT(7,1)|WATER CO2THE AVAILABILITY(7,1)|ALKALINITY(6,2)|ANNULUS(6,2)|FINE POWDER(6,2)|FLUID COMMUNICATION(6,2)|FLUID INJECTION(6,2)|GAS MANIFOLD(6,2)|HEMISPHERE(6,2)|REAGENT(6,2)|SEAWATER(6,2)|BOOSTER PUMP(5,4)|DOSING PUMP(5,4)|INFUSION PUMP(5,4)|MAXIMUM DEPTH(5,4)|CLOGGING(5,2)|CONTROL PANEL(5,2)|ACCURATE CALCULATION(5,1)|BORE CASING(5,1)|CARBON DIOXIDE SEGREGATION(5,1)|CO2 OLIVINE REACTION(5,1)|CO2COMPLETELY(5,1)|CONCENTRATION TREND(5,1)|DISSOLVED OBSERVED BOREHOLE FLUID(5,1)|ELECTRICITY GENERATION(5,1)|FLOTATION TREATMENT(5,1)|FLUID MIXTURE2IN(5,1)|FOSSIL FUEL CONSUMPTION(5,1)|GEOLOGICAL TIMESCALE(5,1)|HYBRID CONTROLLER(5,1)|IMPURITY ACID LEACHING REMOVAL(5,1)|INFLATE AQUEOUS SOLUTION(5,1)|INFLOW INJECTION FLUID PORT(5,1)|INJECTED FLUID HOMOGENEOUS NATURE(5,1)|INJECTION ZONE DURATION(5,1)|INSTALLATION DEPTH(5,1)|INSTRUMENTALITY(5,1)|OLIVINE MAGNESIUM OXIDE(5,1)|PRESSURIZED STREAM(5,1)|REDUCED ENVIRONMENTAL IMPACT2THERE(5,1)|REGION CONTAMINATION(5,1)|REMOVING IMPURITY(5,1)|RETURN BOREHOLE WALL(5,1)|RUN SCHEDULE(5,1)|SERPENTINE REACTANT TEMPERATURE(5,1)|SETPOINT(5,1)|SILICATE MINERAL WEATHERING RATE(5,1)|SOLAR OFF GRID OPERATION(5,1)|SOLID CARBONATE MINERAL(5,1)|TOTAL MINERALIZATION(5,1)|LOW PRESSURE ZONE(4,4)|CARBONIC ACID(4,3)|GROUND STORAGE TANK(4,3)|MANGANESE(4,3)|RETURN FLUID PIPE(4,3)|2CO22MGCO(4,1)|ACIDIC AQUEOUS SOLUTION(4,1)|ATMOSPHERIC CARBON DIOXIDE CONVERSION(4,1)|BASALT(4,1)|BIOFUEL(4,1)|BIOMASS(4,1)|BOREHOLE LINEAR DISTANCE(4,1)|BOREHOLE WATER(4,1)|BRILLIANT REACTION PATH(4,1)|BRILLITE(4,1)|BUOYANCY(4,1)|BURDEN(4,1)|CACO3CONVERTED(4,1)|CAMGSI2O(4,1)|CARBON CAPTURE MODULE(4,1)|CARBON DIOXIDE INJECTION MODULE(4,1)|CARBON ISOLATION(4,1)|CENTURY2IT(4,1)|CO2 OLIVINE LAYER(4,1)|CO2ALTHOUGH(4,1)|CO2ARE(4,1)|CO2DISTANCE(4,1)|CO2MINIMIZES WATER CONSUMPTION(4,1)|CO2RELATIVE(4,1)|CO2STORAGE(4,1)|CO2WATER(4,1)|CONNECTOR COUPLING(4,1)||(CA3191648)|CARBON DIOXIDE(100,38)|CARBON DIOXIDE SEQUESTRATION(100,11)|RENEWABLE ENERGY SOURCE(100,10)|IN SITU MINERALIZATION(100,2)|NATURAL PERIDOTITE CARBONATION(100,1)|PERIDOTITE IN SITU MINERALIZATION(100,1)|PACKER MODULE(90,3)|ROCK FORMATION(87,16)|SEQUESTRATION(61,2)|INJECTION TUBING(61,1)|SYNCHRONIZED BIOFUEL GENERATOR(61,1)|PERIDOTITE(58,15)|CO2 MINERALIZATION(58,2)|GAS DISSOLUTION MODULE(57,9)|MIXTURE EJECTION(54,1)|PERFORATION(53,11)|PERIDOTITE ROCK(52,4)|PERMANENTLY SEQUESTERING CARBON DIOXIDE(52,1)|BIO FUEL GENERATOR(50,4)|CO2 RICH INJECTION(47,5)|FINANCIAL TERM(44,1)|SOLAR INVERTER(44,1)|INJECTION INTERVAL HYDRAULIC ISOLATION(42,1)|SUBSURFACE MODULE(42,1)|CO2 RICH(41,19)|RECYCLING WATER(41,1)|SOLAR PHOTOVOLTAIC PANEL(39,1)|STORE CO2(39,1)|PERMEABLE ZONE(38,1)|CARBON CAPTURE PLANT(35,1)|INFLATE AQUEOUS SOLUTION(35,1)|BIO FUEL ENERGY(32,1)|LIVE MONITORING(31,2)|HYBRID RENEWABLE(30,2)|PERMANENT CARBON DIOXIDE(30,1)|REACTION PATHWAY(29,5)|MAGNESITE(29,4)|CALCITE(28,3)|PERMEABILITY(27,2)|MINIMUM LM(27,1)|CO2(26,39)|CARBON STORAGE(26,1)|DOWNSTREAM PRESSURE(26,1)|IDENTIFIED DEPTH(26,1)|LENGTH PERFORATION(25,1)|SOLAR ENERGY MODULE(25,1)|INJECTION WELL TUBING(24,5)|CARBON FOOTPRINT(23,1)|HYDROELECTRICITY(23,1)|NONCORROSIVE INJECTION WELL TUBING(23,1)|SOLAR CELL(22,1)|NONCORROSIVE WELL CASING(20,1)|RECYCLING WATER RECYCLED BACK(19,1)|PERIDOTITE VOLUME(18,7)|CO2 DISSOLUTION(17,7)|CARBON DIOXIDE SOURCE(17,1)|FLUID VOLUME(17,1)|GEOTHERMAL ENERGY(17,1)|NONCORROSIVE WELL INJECTION TUBING(17,1)|RENEWABLE POWER(17,1)|WIRING(17,1)|OBSERVATION WELL(16,4)|RENEWABLE ENERGY(16,3)|GLOBAL WAFFLING SUPPRESSION(16,1)|HYDROSTATIC PRESSURE SENSOR(16,1)|MONITORING BOREHOLE(15,4)|WIND TURBINE(15,3)|INJECTION POINT(14,2)|PERIDOTITE RESERVOIR(14,2)|ARTIFICIAL CONSERVATIVE TRACER(14,1)|ATMOSPHERIC AIR(14,1)|CARBON FOOTPRINT LOW(14,1)|GAS FLOW(14,1)|HYDRO ENERGY(14,1)|MINIMUM TEMPERATURE(14,1)|SURFACE PACKER CONTROLLER(14,1)|INJECTION WELL(13,18)|ESTIMATING CO2 MINERALIZATION CAPACITY(13,1)|HYBRID ENERGY SOURCE(13,1)|INJECTED CONSERVATIVE TRACER(13,1)|INJECTION BOREHOLE DEEP PERFORATION(13,1)|INJECTION BOREHOLE PERFORATION(13,1)|MAGNESIA PERIDOTITE ORE PRODUCTION(13,1)|NONCALCINATED PERIDOTITE(13,1)|NONCORROSIVE CASING PERMANENT INSTALLATION(13,1)|OLIVINE CARBONATION(13,1)|PERFORATION CAREFUL PLACEMENT(13,1)|PERIDOTITE CARBONATION(13,1)|PERIDOTITE MINERALIZATION(13,1)|PERIDOTITE NATURAL CARBONATION(13,1)|PERIDOTITE REACTIVITY(13,1)|POLLUTANT REMEDIATION(13,1)|PYROXENE MINERAL LESSER PROPORTION(13,1)|RENEWABLE ENERGY STORAGE MODULE(12,2)|SUBMERSIBLE PUMP(11,13)|PACKED OFF INTERVAL(11,4)|TARGET INJECTION ZONE(11,4)|AMBIENT RESERVOIR GROUNDWATER(11,1)|DATA ACQUISITION(11,1)|FLOWING MIXTURE(11,1)|GREEN ENERGY SOURCE(11,1)|PERIDOTITE IGNEOUS ROCK(11,1)|RECOVERY BOREHOLE COLLECT(11,1)|SWITCH GEAR(11,1)|TECTONICALLY EXPOSED PERIDOTITE(11,1)|WIND ENERGY(11,1)|WELL CASING(10,6)|PACKER TOOL(10,2)|CO2 EFFERVESCENCE(10,1)|CO2 LATE INJECTION(10,1)|DEEP BOREHOLE(10,1)|DOWNHOLE INJECTION PIPING(10,1)|FIXATION CO2 ABSORPTION(10,1)|GLACIER RETREAT(10,1)|H2S ABATEMENT(10,1)|INJECTED CO2 RICH MONITORING(10,1)|INOSILICATE MINERAL(10,1)|MANTLE PERIDOTITE(10,1)|OBSERVED CLIMATE CHANGEOVER(10,1)|POLLUTANT SUPPRESSION(10,1)|RECONNAISSANCE MAPPING(10,1)|RECOVERING BOREHOLE(10,1)|RETURN FLUID WELL(10,1)|SENSITIVE THERMODYNAMIC BEHAVIOR(10,1)|SERPENTINE REACTANT(10,1)|STANDBY WING(10,1)|SUBMERSIBLE INTAKE PUMP(10,1)|SUBSURFACE CONNECTIVITY(10,1)|CO2 MOLAR RATIO(9,3)|OLIVINE REACTION(9,2)|POROSITY(8,4)|CO2 TANK(8,2)|PERIDOTITE LAYER(8,2)|TRACER FLUID(8,2)|ABUNDANT MINERAL(8,1)|ANTHROPOGENIC IMPACT(8,1)|BUFFER TANK SIZING(8,1)|BULK ROCK FRACTURE STRESS(8,1)|CO2 COLLISION(8,1)|CO2 FIXATION DECREASE(8,1)|CO2 RICH RELEASE(8,1)|DARCY LAW(8,1)|DISSOLVED CO2 SOLUBILITY(8,1)|DOWNSTREAM END(8,1)|EARTH MANTLE(8,1)|ENERGY SOURCE(8,1)|GAS INFLATION PACKER(8,1)|GEOLOGICAL RESERVOIR(8,1)|HYDROUS ALTERATION PRODUCT(8,1)|INJECTION BOREHOLE WALL(8,1)|LIQUID CONSERVATIVE TRACER(8,1)|LITER PER MINUTE(8,1)|MAGNESIA PURITY(8,1)|MG CARBONATION(8,1)|MINERAL OLIVINE(8,1)|NONCORROSIVE PIPE(8,1)|OBSERVATION BOREHOLE FLUID(8,1)|OUTGOING SAMPLING PORT(8,1)|PERFORATION DEPTH(8,1)|PERIDOTITE PERMEABLE LAYER(8,1)|PERIDOTITE ROCK FORMATION(8,1)|POLYMER TUBING STRING(8,1)|PROGRAM REPORT(8,1)|RECOVERY BOREHOLE DEPTH(8,1)|SOLUBILIZED CO2(8,1)|SUPPRESSING GLOBAL WARMING(8,1)|UNINTERRUPTED CO2(8,1)|UNINTERRUPTED DRAW(8,1)|UPSTREAM END(8,1)|FLUID INJECTION(7,3)|ACCURATE ACCOUNTING(7,1)|BIO FUEL MODULE(7,1)|BOREHOLE FULL DEPTH(7,1)|BURNING FOSSIL FUEL(7,1)|CARBONATE ROCK(7,1)|CARBONATION REACTION(7,1)|CO2 EMISSION(7,1)|DILUTION CALCULATION(7,1)|DISSOLVED CO2 ANALYSIS(7,1)|DOMINANT INFLUENCE(7,1)|INJECTION PIPELINE(7,1)|INJECTION PORTABILITY(7,1)|MAXIMIZE BUBBLE(7,1)|MINERALIZATION REACTION(7,1)|MINIMAL INTERRUPTION(7,1)|MONITORING OBSERVATION BOREHOLE(7,1)|NATURAL FRACTURE NETWORK(7,1)|NATURAL TRACER(7,1)|PAST CENTURY(7,1)|PAST DECADE(7,1)|PERIDOTITE GEOLOGIC FORMATION(7,1)|SEA FLOOR(7,1)|STABLE CARBONATE MINERAL(7,1)|SUBTERRANEAN GEOLOGIC FORMATION(7,1)|TARGET SETPOINT(7,1)|TRACER MOLAR RATIO(7,1)|TRACER SUBSTANCE(7,1)|UNDISSOLVED CO2 GAS BUBBLE(7,1)|PHOTOVOLTAIC(6,3)|ATMOSPHERIC CO2(6,2)|BLOCKAGE(6,2)|FINE POWDER(6,2)|H2S GAS BUBBLE(6,2)|INTERMITTENCY(6,2)|LOW PRESSURE ZONE(6,2)|MG3SI2O(6,2)|PRETREATMENT(6,2)|REAGENT(6,2)|SEAWATER(6,2)|TARGET FORMATION(6,2)|BOOSTER PUMP(5,4)|DOSING PUMP(5,4)|AQUEOUS SOLUTION(5,3)|CACO3(5,3)|CARBONIC ACID(5,3)|PRESSURIZED WATER STREAM(5,3)|RETURN FLUID PIPE(5,3)|DRILLING(5,2)|ABSORPTION ENHANCEMENT(5,1)|ACCELERATE REMOVAL(5,1)|ALTERATION NATURE(5,1)|ARTIFICIALLY PRODUCED CA(5,1)|ATMOSPHERIC CARBON DIOXIDE YEAR(5,1)|BOREHOLE SINGLE HEMISPHERE(5,1)|BUOYANCY(5,1)|CHEMICAL WEATHERING ACCELERATION(5,1)|CO2 EMITTING INDUSTRY(5,1)|CO2 PERIDOTITE REACTION(5,1)|CO2 PYROXENE REACTION(5,1)|CO2 STORAGE FACILITY(5,1)|CONTROL PANEL(5,1)|DAMPENING PRESSURE FLUCTUATION(5,1)|FLUID FLOWPATH(5,1)|FOSSIL FUEL CONSUMPTION(5,1)|FUZED PHOSPHATE(5,1)|GEOLOGICAL FORMATION TARGET ZONE(5,1)|HEAD UNIT(5,1)|HOMOGENEOUS NATURE(5,1)|HYBRID CONTROLLER(5,1)|HYDRAULIC COMMUNICATION(5,1)|INCOMING INJECTION FLUID(5,1)|INJECTED FLUID HOMOGENOUS NATURE(5,1)|INJECTION ZONE INTERVAL(5,1)|INSTRUMENTALITY(5,1)|INTERMITTENT NATURE(5,1)|ISOLATED INJECTION INTERVAL(5,1)|LIMITING NATURAL FRACTURE(5,1)|MAGNESIUM SINKING PROCESSING(5,1)|MAGNETIC BEHAVIOR(5,1)|MONITORING MODULE(5,1)|NIGHT LOAD(5,1)|NONCORROSIVE FLUID PIPE(5,1)|OVERPRESSURE(5,1)|PERIDOTITE FORMATION ILLUSTRATION(5,1)|PERIDOTITE MAGNESIUM OXIDE(5,1)|PERIDOTITE MAXIMUM DEPTH(5,1)|PERMEABILITY TEST(5,1)|PLACEMENT DEPTH(5,1)|PRIMARY WING(5,1)|REMOVING IMPURITY(5,1)|RETURN BOREHOLE WALL(5,1)|SEQUESTERING CARBON DIOXIDE(5,1)|SHUTINTOOL(5,1)|SIZE WELL INJECTION TUBING(5,1)|SOLID CARBONATE MINERAL(5,1)|SUBSURFACE FORMATION(5,1)|TARGET INJECTION INTERVAL(5,1)|TREATING CO2(5,1)|UNDERGROUND ROCK FORMATION(5,1)|UNIFORM BEHAVIOR(5,1)|UNITED NATIONS ENVIRONMENT(5,1)|UPWARD DRIFT(5,1)|INJECTION PUMP(4,4)|ALKALINITY(4,1)|AMPHIBOLITE(4,1)|ANNULUS SPACE(4,1)|AQUEOUS ACIDIC SOLUTION(4,1)|ATMOSPHERIC CARBON DIOXIDE CONVERSION(4,1)|AVIATION(4,1)|BASALT(4,1)|BIOMASS(4,1)|BOREHOLE WATER(4,1)|BUBBLE DIAMETER(4,1)|CA2MG5SI8O(4,1)|CAMGSI2O(4,1)|CAMGSIO(4,1)|CARBON CAPTURE MODULE(4,1)|CARBON DIOXIDE INJECTION MODULE(4,1)|CO2 ABATEMENT DEGREE(4,1)|CO2 EMITTING INDUSTRIAL PLANT(4,1)|CO2 FIXATION(4,1)|CO2 LOSS(4,1)|CO2 SATURATED FLUID(4,1)||(AU2022209209)|CARBON DIOXIDE(100,48)|RENEWABLE ENERGY SOURCE(100,20)|CARBON DIOXIDE SEQUESTRATION(100,12)|IN SITU MINERALIZATION(100,4)|PERIDOTITE IN SITU MINERALIZATION(100,2)|ROCK FORMATION(99,23)|NATURAL PERIDOTITE CARBONATION(80,1)|PACKER MODULE(63,6)|INJECTION TUBING(63,2)|MIXTURE EJECTION(55,2)|PERIDOTITE ROCK FORMATION(54,5)|GAS DISSOLUTION MODULE(50,14)|PERIDOTITE(48,14)|MAGNESITE(42,5)|CO2 MINERALIZATION(42,3)|RECYCLING WATER(42,3)|PERMANENTLY SEQUESTERING CARBON DIOXIDE(42,1)|SYNCHRONIZED BIOFUEL GENERATOR(41,2)|CO2 RICH INJECTION(39,3)|PERFORATION(38,16)|BIO FUEL GENERATOR(37,6)|CALCITE(37,5)|FINANCIAL TERM(35,1)|NATURAL WEATHERING(35,1)|CO2 RICH(33,20)|CARBONATE ROCK(29,2)|MINERALIZATION REACTION(29,2)|SUBSURFACE MODULE(29,2)|SOLAR INVERTER(28,3)|INJECTION INTERVAL HYDRAULIC ISOLATION(28,2)|CARBON CAPTURE PLANT(28,1)|SOLAR PHOTOVOLTAIC PANEL(26,2)|PERMEABLE ZONE(25,2)|SEQUESTRATION(25,2)|HYBRID RENEWABLE(24,2)|NONCORROSIVE INJECTION WELL TUBING(24,2)|PERMANENT CARBON DIOXIDE(24,1)|LIVE MONITORING(23,3)|CO2(22,46)|INJECTION WELL TUBING(22,10)|REACTION PATHWAY(22,6)|BIO FUEL ENERGY(21,2)|CARBON STORAGE(21,1)|DOWNSTREAM PRESSURE(21,1)|IDENTIFIED DEPTH(21,1)|NONCORROSIVE WELL CASING(20,2)|OBSERVATION WELL(19,9)|CARBON FOOTPRINT(18,1)|ENERGY EXPENDITURE(17,1)|SOLAR ENERGY MODULE(16,2)|PERIDOTITE VOLUME(15,7)|CO2 DISSOLUTION(14,7)|PERIDOTITE MINERALIZATION(14,2)|CARBON DIOXIDE SOURCE(14,1)|PERIDOTITE SITU CARBONATION(14,1)|RENEWABLE SOURCE(14,1)|INJECTION WELL(13,28)|MGCO3(12,4)|MONITORING BOREHOLE(12,4)|RENEWABLE ENERGY(12,4)|PERIDOTITE FORMATION(11,5)|HYDROELECTRIC POWER(11,4)|WIND TURBINE(11,4)|FLUID VOLUME(11,2)|GEOTHERMAL ENERGY(11,2)|INJECTION POINT(11,2)|PERIDOTITE RESERVOIR(11,2)|WIRING(11,2)|ARTIFICIAL CONSERVATIVE TRACER(11,1)|ATMOSPHERIC AIR(11,1)|CARBON FOOTPRINT LOW(11,1)|GAS FLOW(11,1)|MINERALIZATION TIME(11,1)|PERIDOTITE LAYER(10,5)|HYDROSTATIC PRESSURE SENSOR(10,2)|INJECTED CONSERVATIVE TRACER(10,1)|INJECTION BOREHOLE DEEP PERFORATION(10,1)|INJECTION BOREHOLE PERFORATION(10,1)|MAGNESIA PERIDOTITE ORE PRODUCTION(10,1)|NONCORROSIVE CASING PERMANENT INSTALLATION(10,1)|OLIVINE CARBONATION(10,1)|PERFORATION CAREFUL PLACEMENT(10,1)|PERIDOTITE CARBONATION(10,1)|PERIDOTITE NATURAL CARBONATION(10,1)|PERIDOTITE REACTIVITY(10,1)|POLLUTANT REMEDIATION(10,1)|PYROXENE MINERAL LESSER PROPORTION(10,1)|SUBMERSIBLE PUMP(9,15)|PACKED OFF INTERVAL(9,5)|TARGET INJECTION ZONE(9,4)|MINIMUM TEMPERATURE(9,2)|NONCORROSIVE PIPE(9,2)|RENEWABLE ENERGY STORAGE MODULE(9,2)|SURFACE PACKER CONTROLLER(9,2)|AMBIENT RESERVOIR GROUNDWATER(9,1)|PERIDOTITE IGNEOUS ROCK(9,1)|RECOVERY BOREHOLE COLLECT(9,1)|TECTONICALLY EXPOSED PERIDOTITE(9,1)|HYBRID ENERGY SOURCE(8,2)|PACKER TOOL(8,2)|SEALING LENGTH(8,2)|CO2 EFFERVESCENCE(8,1)|CO2 LATE INJECTION(8,1)|CO2 MINERALIZATION CAPACITY(8,1)|DEEP BOREHOLE(8,1)|DOWNHOLE INJECTION PIPING(8,1)|FIXATION CO2 ABSORPTION(8,1)|GLACIER RETREAT(8,1)|H2S ABATEMENT(8,1)|INJECTED CO2 RICH MONITORING(8,1)|INOSILICATE MINERAL(8,1)|MANTLE PERIDOTITE(8,1)|MINERALIZATION OCCURRENCE(8,1)|OBSERVED CLIMATE CHANGEOVER(8,1)|PERIDOTITE TARGET ZONE(8,1)|POLLUTANT SUPPRESSION(8,1)|RECONNAISSANCE MAPPING(8,1)|RECOVERING BOREHOLE(8,1)|RETURN FLUID WELL(8,1)|SENSITIVE THERMODYNAMIC BEHAVIOR(8,1)|SERPENTINE REACTANT(8,1)|STANDBY WING(8,1)|SUBMERSIBLE INTAKE PUMP(8,1)|SUBSURFACE CONNECTIVITY(8,1)|CO2 MOLAR RATIO(7,3)|DATA ACQUISITION(7,2)|FLOWING MIXTURE(7,2)|GREEN ENERGY SOURCE(7,2)|OLIVINE REACTION(7,2)|SWITCH GEAR(7,2)|WIND ENERGY(7,2)|ABUNDANT MINERAL(7,1)|ANTHROPOGENIC IMPACT(7,1)|BUFFER TANK SIZING(7,1)|BULK ROCK FRACTURE STRESS(7,1)|CO2 COLLISION(7,1)|CO2 FIXATION DECREASE(7,1)|CO2 RICH RELEASE(7,1)|DARCY LAW(7,1)|DISSOLVED CO2 SOLUBILITY(7,1)|EARTH MANTLE(7,1)|GAS INFLATION PACKER(7,1)|GEOLOGICAL RESERVOIR(7,1)|GLOBAL WARMING SUPPRESSION(7,1)|HYDROUS ALTERATION PRODUCT(7,1)|INJECTION BOREHOLE WALL(7,1)|LIQUID CONSERVATIVE TRACER(7,1)|MAGNESIA PURITY(7,1)|MG CARBONATION(7,1)|MINERAL OLIVINE(7,1)|MINERALIZATION SITE(7,1)|OBSERVATION BOREHOLE FLUID(7,1)|OUTGOING SAMPLING PORT(7,1)|PERFORATION DEPTH(7,1)|PERIDOTITE PERMEABLE LAYER(7,1)|POLYMER TUBING STRING(7,1)|PROGRAM REPORT(7,1)|RECOVERY BOREHOLE DEPTH(7,1)|SOLUBILIZED CO2(7,1)|UNINTERRUPTED CO2(7,1)|UNINTERRUPTED DRAW(7,1)|POROSITY(6,4)|FLUID INJECTION(6,3)|CO2 TANK(6,2)|DOWNSTREAM END(5,2)|UPSTREAM END(5,2)|ACCURATE ACCOUNTING(5,1)|BIO FUEL MODULE(5,1)|BOREHOLE FULL DEPTH(5,1)|BURNING FOSSIL FUEL(5,1)|CACO3 SIO2(5,1)|CAPTURED CO2(5,1)|CARBONATION REACTION(5,1)|CO2 EMISSION(5,1)|DISSOLVED CO2 ANALYSIS(5,1)|DOMINANT INFLUENCE(5,1)|GENERATOR SYNCHRONIZATION(5,1)|INJECTING CO2(5,1)|INJECTION PIPELINE(5,1)|INJECTION PORTABILITY(5,1)|MAXIMIZE BUBBLE(5,1)|MINIMAL INTERRUPTION(5,1)|MONITORING OBSERVATION BOREHOLE(5,1)|NATURAL FRACTURE NETWORK(5,1)|NATURAL TRACER(5,1)|PAST CENTURY(5,1)|PAST DECADE(5,1)|PERIDOTITE GEOLOGIC FORMATION(5,1)|PERIDOTITEWATER REACTION(5,1)|PILOT SCALE EXPERIMENT(5,1)|SEA FLOOR(5,1)|STABLE CARBONATE MINERAL(5,1)|SUBTERRANEAN GEOLOGIC FORMATION(5,1)|TARGET SETPOINT(5,1)|TRACER MOLAR RATIO(5,1)|TRACER SUBSTANCE(5,1)|TRACER TANK(5,1)|TRAPPING CO2(5,1)|UNDISSOLVED CO2 GAS BUBBLE(5,1)|WELL CASING(4,11)|BOOSTER PUMP(4,4)|DOSING PUMP(4,4)|MBGL(4,4)|CARBONIC ACID(4,3)|MANGANESE(4,3)|PRESSURIZED WATER STREAM(4,3)|RETURN FLUID PIPE(4,3)|ALKALINITY(4,2)|ATMOSPHERIC CO2(4,2)|BIOFUEL(4,2)|BLOCKAGE(4,2)|DILUTION(4,2)|DRILLING(4,2)|FINE POWDER(4,2)|GAS DISSOLUTION(4,2)|H2S GAS BUBBLE(4,2)|INTERMITTENCY(4,2)|MG3SI2O(4,2)|PRETREATMENT(4,2)|REAGENT(4,2)|SEAWATER(4,2)|TARGET FORMATION(4,2)|ABSORPTION ENHANCEMENT(4,1)|ACCELERATE REMOVAL(4,1)|ALTERATION NATURE(4,1)|ARTIFICIALLY PRODUCED CA(4,1)|ATMOSPHERIC CARBON DIOXIDE YEAR(4,1)|BOREHOLE SINGLE HEMISPHERE(4,1)|BUOYANCY(4,1)|CHEMICAL WEATHERING ACCELERATION(4,1)|CO2 EMITTING INDUSTRY(4,1)|CO2 PERIDOTITE REACTION(4,1)|CO2 PYROXENE REACTION(4,1)|CO2 STORAGE FACILITY(4,1)|COMPRESSED CO2(4,1)|CONTACTOR(4,1)|DAMPENING PRESSURE FLUCTUATION(4,1)|FEEDING CO2(4,1)|FOSSIL FUEL CONSUMPTION(4,1)|FUZED PHOSPHATE(4,1)|GEOLOGICAL FORMATION TARGET ZONE(4,1)|HOMOGENEOUS NATURE(4,1)|HYBRID CONTROLLER(4,1)|HYDRAULIC COMMUNICATION(4,1)|INCOMING INJECTION FLUID(4,1)|INFLATE AQUEOUS SOLUTION(4,1)|INJECTED FLUID HOMOGENOUS NATURE(4,1)|INJECTION ZONE INTERVAL(4,1)|INSTRUMENTALITY(4,1)|INTERMITTENT NATURE(4,1)|ISOLATED INJECTION INTERVAL(4,1)|LIMITING NATURAL FRACTURE(4,1)|MAGNESIUM SINKING PROCESSING(4,1)|MAGNETIC BEHAVIOR(4,1)|MONITORING MODULE(4,1)|NIGHT LOAD(4,1)|NONCORROSIVE FLUID PIPE(4,1)|NUCLEOTIDE(4,1)|OVERPRESSURE(4,1)|PERIDOTITE MAGNESIUM OXIDE(4,1)|PERIDOTITE MAXIMUM DEPTH(4,1)|PERMEABILITY TEST(4,1)|PLACEMENT DEPTH(4,1)|PRIMARY WING(4,1)|REMOVING IMPURITY(4,1)|RETURN BOREHOLE WALL(4,1)|SOLID CARBONATE MINERAL(4,1)|SUBSURFACE FORMATION(4,1)|TARGET INJECTION INTERVAL(4,1)|TRACER FLUID(4,1)|TREATING CO2(4,1)|UNDERGROUND ROCK FORMATION(4,1)|UNIFORM BEHAVIOR(4,1)|UNITED NATIONS ENVIRONMENT(4,1)|UPWARD DRIFT(4,1)|INJECTION PUMP(3,4)|LOW PRESSURE ZONE(3,4)|AMPHIBOLITE(3,1)|ANNULUS SPACE(3,1)|AQUEOUS ACIDIC SOLUTION(3,1)|ATMOSPHERIC CARBON DIOXIDE CONVERSION(3,1)|AVIATION(3,1)|BASALT(3,1)|BIOMASS(3,1)|BOREHOLE WATER(3,1)|BPS(3,1)|BUBBLE DIAMETER(3,1)|CA2MG5SI8O(3,1)|CAMGSI2O(3,1)|CAMGSIO(3,1)|CARBON CAPTURE MODULE(3,1)|CARBON DIOXIDE INJECTION MODULE(3,1)|CO2 ABATEMENT DEGREE(3,1)|CO2 EMITTING INDUSTRIAL PLANT(3,1)|CO2 FIXATION(3,1)|CO2 LOSS(3,1)|CO2 SATURATED FLUID(3,1)|CO2 STORAGE TANK(3,1)|CO2 WATER TARGETED INJECTION(3,1)|CONFIRMATION(3,1)|CREVICE(3,1)|DAYTIME(3,1)|DOSING RATE(3,1)|DROUGHT(3,1)|DUNITE(3,1)|ELECTRICAL STORAGE FACILITY(3,1)|ELECTRICITY(3,1)| (EP4134513)|1. A method of carbon dioxide sequestration by in situ mineralization characterized in that:| an amount of carbon dioxide is dissolved into water to form a carbon dioxide and water mixture;| an amount of said carbon dioxide and water mixture is injected into a rock formation comprising peridotite via an injection well (220, 320, 1020), wherein the carbon dioxide and water mixture is flowed through said injection well having a non-corrosive well casing and a non-corrosive injection well tubing disposed in the rock formation, and at least one packer creating a packed off interval, said injection well tubing having a plurality of longitudinal perforations at a depth of 0.4 to 4 km in said rock formation;| a high-pressure zone is created within said injection well (220, 320, 1020) below said packed off interval,| water from said rock formation is recycled via an observation well (230, 330, 1030) creating a low-pressure zone during said recycling through the observation well (230, 330, 1030). ;| carbon dioxide in said carbon dioxide and water mixture is reacted with said rock formation to form calcites and magnesites, and| all steps of the process are powered by a renewable energy source.|2. The method of carbon dioxide sequestration of claim 1, wherein said injection and observation wells have the same depth.|3. The method of carbon dioxide sequestration of claim 1, wherein said longitudinal perforations have a length (l) of at least 15 cm and the density of said perforations along the injection well tubing and, optionally, a well casing in the injection well (220, 320, 1020), are chosen depending on the fluid flow rate at the permeable zones.|4. The method of carbon dioxide sequestration of claim 1, wherein said high pressure zone is used to inject said carbon dioxide and water mixture into said injection well at depth between 0.8 to 1.2 km.|5. The method of carbon dioxide sequestration of claim 1, wherein said renewable energy source is selected from the group consisting of solar energy, wind energy, biofuel energy, hydroelectric power, geothermal energy and other green energy sources.|6. The method of carbon dioxide sequestration of claim 1, further comprising a step of recycling water back to a storage tank (340).|7. The method of carbon dioxide sequestration of claim 6, wherein during the injecting, a high-pressure zone is created within said injection well (220, 320, 1020) below a packed off interval and a low-pressure zone is created during the recycling through the observation well (230, 330, 1030).|8. The method of carbon dioxide sequestration of claim 7, wherein most of the carbon dioxide and water mixture flows from a high- to a low-pressure zone and most of fluid volume is recycled back through the observation well (230, 330, 1030).|9. A system for controlled enhancement of peridotite in situ mineralization characterized in that said system comprises:| an injection well (220, 320, 1020) bored in a rock formation comprising peridotite and having a non-corrosive well casing;| a non-corrosive injection well tubing disposed in said injection well;| a packer module (312, 1012) connected to the injection tubing and disposed in the injection well;| a renewable energy source;| a gas dissolution module (310) connected to the renewable energy source, wherein the gas dissolution module includes a carbon dioxide and water mixture ejection port,| and wherein all steps are powered by the renewable energy source.|10. The system of claim 9, wherein the packer module (312, 1012) is an inflatable unit for hydraulic isolation of an injection interval at an identified depth in the injection well (220, 320, 1020).|11. The system of claim 9 wherein the packer (312, 1012) has a minimum 1 m sealing length, and wherein said system comprises| - an on-surface packer controller;| - in-line hydrostatic pressure sensors at an upstream end and a downstream end of said packer;| - an in-line pressure sensor;| - an injection and pumping head units; and| - channels for wiring, data acquisition and live monitoring.|12. The system of claim 9, wherein the renewable energy source is a hybrid energy source selected from the group consisting of a solar energy module; a renewable energy storage module; a wind turbine; hydroelectric power; a biofuel generator; and other renewable energy sources.|13. The system of claim 9, wherein said renewable energy source comprises one or more of: solar photovoltaic panels; solar inverters; synchronized biofuel generators; an energy storage module; and control panels and switch gears.|14. The system of claim 12 or 13, wherein said renewable energy source provides power to on-surface and sub-surface modules.|15. The system of claim 9, wherein the gas dissolution module is installed on the surface for gas transfer of carbon dioxide into water prior to the injection well tubing.|16. The system of claim 15, wherein said gas dissolution module is configured to inject at a gas flow rate of a minimum of 15 litre per minute, a gas pressure of a minimum 800 kPa (8 bar), and a minimum temperature of 20°C. (EP4134513)|TECHNICAL FIELD|[0001] The present disclosure relates to a system and method for permanent carbon dioxide (CO2) sequestration in peridotite rock formations. More specifically, the present disclosure relates to accelerating and controlling natural peridotite carbonation between peridotite and a source of carbon dioxide to be sequestered. The present disclosure also relates to methods for permanently sequestering carbon dioxide that is captured from industrial emissions, atmospheric air, or that contained in bodies of fluid. The present disclosure also relates to the use of renewable sources of energy for carbon capture plants and carbon storage process equipment.|BACKGROUND|[0002] Over the past century, industrial activities, particularly fossil fuel consumption, have caused a dramatic increase of the CO2 concentration in the atmosphere. This anthropogenic impact on the global carbon cycle is the main reason for the observed climate change over the past decades. Global climate change has been linked to various other phenomena, including hurricanes, droughts, floods, glacier retreat, and rising sea levels. A recent United Nations Environment Programme report on global warming indicates that `human influences will continue to change atmospheric composition throughout the 21st century' and carbon dioxide makes the largest contribution out of these human activities. CO2 is released into the atmosphere by the combustion of fossil fuels such as coal, oil or natural gas, and renewable fuels like biomass; by the burning of, for example, forests during land clearance; and from certain industrial and resource extraction processes. As a result, `emissions of CO2 due to fossil fuel burning are virtually certain to be the dominant influence on the trends in atmospheric CO2 concentration during the 21st century' and 'global average temperatures and sea level are projected to rise'.|[0003] As such, large efforts have been made to develop effective carbon capture and storage (CCS) methods that remove CO2 from the atmosphere. Chemical weathering is a slow process that controls atmospheric CO2 concentrations over geological time scales. Several prior art references have proposed accelerating chemical weathering to counter global climate change. The goal of enhanced weathering is to hasten silicate mineral weathering rates to accelerate the removal of CO2 from the atmosphere in the form of dissolved inorganic carbon and/or as carbonate minerals. Because of their relatively rapid dissolution rates, enhanced weathering has focused on mafic and ultramafic rocks.|[0004] Because of its high concentration of Mg, tectonically exposed peridotite from the Earth's upper mantle, which is composed largely of the mineral olivine ((Mg, Fe)SiO4), with lesser proportions of pyroxene minerals ((Mg, Fe, Ca)Si2O) and spinel ((Mg, Fe)(Cr, Al)O), and its hydrous alteration product serpentine (Mg3Si2O5(OH)5), have been considered a promising reactant for conversion of atmospheric carbon dioxide to solid carbonate. Natural carbonation of peridotite has been found to be surprisingly rapid compared to other types of rocks. For example, carbonate veins in mantle peridotite in Oman have an average age of approximately 26,000 years and are not 30 to 95 million years old as previously believed. These data and reconnaissance mappings show that approximately 104 to 105 tons per year of atmospheric carbon dioxide are converted to solid carbonate minerals via peridotite weathering in Oman (Peter B. Kelemen and Jürg Matter, In situ carbonation of peridotite for CO2 storage, PNAS November 11, 2008 105 (45) 17295-17300).|[0005] Mantle peridotite is ordinarily more than 6 km below the seafloor and is strongly out of equilibrium with air and water at the Earth's surface. Its exposure along large thrust faults and along tectonic plate boundaries creates a large reservoir of chemical potential energy. Despite the available chemical potential, engineering techniques for carbon sequestration have many challenges. Engineering solutions involve grinding peridotite to a fine powder, purifying carbon dioxide gas, using reaction vessels at elevated pressure, and/or heating reactants to 100 degrees Celsius or more, and this comes at a substantial financial and energy cost.|[0006] Various methods have been experimentally evaluated, including direct carbonation of olivine and serpentine powders at elevated temperature, dissolution of serpentine or olivine in hydrochloric acid followed by carbonation of Mg and cations in solution, and reaction of olivine and serpentine with carbonic acid (very similar to natural alteration). Reaction kinetics have been found to be too slow for significant sequestration of carbon dioxide unless the olivine or serpentine reactants are raised to more than 100 degrees Celsius, ground to a fine powder, and/or pre-treated at above 600 degrees Celsius to increase reactive surface area. For the most part, because of the requirements for heating and processing, these approaches have been found to be too expensive in financial terms and, more importantly, in energy expenditure, not commercially viable at present.|[0007] US9193594B2 discloses methods and systems for enhancing rates of carbonation of peridotite both in situ and ex situ. In some embodiments, the methods and systems include the following: fracturing a volume of peridotite; heating the volume of peridotite; injecting an adjustable flow of carbon dioxide into the volume of peridotite; injecting bicarbonate materials into the volume of peridotite; and forming carbonate with the volume of peridotite and the carbon dioxide in an exothermic reaction thereby generating a self-sustaining heat source, the heat source heating the volume of peridotite.|[0008] US8524152B2 discloses methods and systems for enhancing rates of in situ carbonation of peridotite. In some embodiments, the methods and systems include the following: fracturing a volume of peridotite in situ; heating the volume of peridotite in situ; injecting carbon dioxide into the volume of peridotite in situ; and forming carbonate in situ with the volume of peridotite and the carbon dioxide.|[0009] US9266061B2 discloses a filter for treating CO2 from a CO2-emitting industrial plant, taking advantage of the fact that peridotite igneous rocks (or material of similar chemical content: basalt, gabbro, dunite, amphibolites, artificially produced Ca, Mg oxides) which are abundant on and close to the Earth's surface, can absorb and contain CO2 gases resultant from industrial activity. This chemical process occurs naturally but has not been utilized to capture high concentrations of CO2 emitted into the atmosphere. Calcium and magnesium oxides of the peridotite react with CO2 to form stable carbonate minerals. The invention enhances and expedites this natural process for the remediation of industrial pollutants such as CO2 from the oil, gas, coal, cement/concrete and like CO2-emitting industries, and provides a resource for materials in construction (concrete), steel, aviation and agricultural and other industries.|[0010] JP2007283279A discloses a global warming suppression technology for decomposing, insolubilizing, and/or purifying soil polluted by hazardous substances and pollutants such as waste products, and the like, suppressing pollutants at the levels or lower than environmental quality standards for soil over long periods, and naturally adsorbing and decomposing carbon dioxide in air via its reaction step during treatment. A pollutant treating agent containing non-calcinated peridotite as a principal component is used for separating and/or decomposing pollutants in addition to perform long-term in solubilization by adding and/or mixing light-burned magnesite, light-burned dolomite, fused phosphate, or calcined shell powder according to types of pollutant. Thus, the polluted area is purified. Furthermore, the agent absorbs a large amount of carbon dioxide in air during the step of using the agent, so that the agent has effects as a low-cost and low-environmental-load-type technique for suppressing global warming.|[0011] CN108658104A discloses a magnesium sinking technique during a kind of peridotite ore production of magnesia, including processing steps such as ore dressing, grinding, purification and impurity removal, flotation processing, magnesium sinking processing, acid leach removal of impurities, flotation purifying, precipitate separation, to increase the purity and recovery rate of magnesia. The method is disclosed to provide a magnesia purity of up to 99.7% or more, and up to 89.7 94.2%.|[0012] PCT/EP2020/064306 (WO/2020/234464) discloses a method and a system of abating carbon dioxide (CO2) and/or hydrogen sulfide (H2S) in a geological reservoir. Water is pumped or transferred from a water source to an injection well. The gasses are merged with the water under conditions where the hydraulic pressure of the water is less than the pressure of CO2 and/or H2S gas at the merging point. The water with CO2 and/or H2S gas bubbles is transferred further downwardly at a certain velocity higher than the upward flow velocity of said CO2 and/or H2S gas bubbles ensuring downward movement of gas bubbles resulting in full dissolution of said CO2 and/or H2S in the water due to elevating pressure. The complete dissolution ensures a lowered pH of the water entering a geological (e.g. geothermal) reservoir which is needed to promote mineral reactions leading to CO2 and H2S abatement. This abatement may be quantified by dissolving a tracer substance in a predetermined molar ratio to said dissolved CO2 and/or H2S and monitored in a monitoring well.|[0013] A process disclosed by D.E.Clark et al. ("CarbFix2: CO2 and H2S mineralization during 3.5 years of continuous injection into basaltic rocks at more than 250°C" by Deidre E. Clark et al., published in Geochimica et Cosmochimica Acta, volume 279, 1 June 2020, pages 45-66) involves the separation of CO2 and H2S from a geothermal exhaust gas stream, dissolution of the separated CO2 and H2S into a condensed waste stream from said geothermal power plant, injection of the gas-charged condensate to a specific depth in the injection well, using a stainless steel pipe installed inside the injection well casing. In addition, effluent water from the geothermal plant is injected into the injection well in order to drag down (wash down) the gas-charged condensate to the target injection depth. There remains a need for improved methods and systems for efficient and practical CO2 mineralization in large scale and with reduced environmental impact.|SUMMARY|[0014] The present disclosure provides an efficient and controlled method for CO2 mineralization into peridotite rocks using renewable energy. Peridotite rocks are known for comprising mostly silicate minerals such as olivine and pyroxene. These types of minerals are active in the presence of solubilized CO2 producing various carbonate rocks. The present disclosure is based on the idea of injecting solubilized carbon dioxide (water-CO2 mixture) into peridotite rock formations and creating efficient reaction pathways by manipulating the operation conditions (temperature and pressure) for the mineralization reaction to happen. Consequently, CO2 be converted into magnesite (MgCO3) and calcite (CaCO3) and stored permanently in the rock formation in mineral form.|[0015] A first aspect relates to a method of carbon dioxide sequestration by in situ mineralization comprising the steps of| dissolving an amount of carbon dioxide into water to form a carbon dioxide and water mixture;| injecting an amount of said carbon dioxide and water mixture into a rock formation comprising peridotite via an injection well, wherein the carbon dioxide and water mixture is flowed through the injection well or an injection well tubing disposed in the rock formation, the injection well and/or injection well tubing having a plurality of longitudinal perforations at a depth of 0.4 to 4 km in the rock formation;| recycling water from said rock formation via an observation well; and| reacting carbon dioxide in said carbon dioxide and water mixture with said rock formation to form calcites and magnesites, and| all steps of the process are powered by a renewable energy source.|[0016] According to an example not forming part of the present invention, said rock formation consists mainly of peridotite.|[0017] According to an embodiment, said injection and observation wells have the same depth.|[0018] According to an embodiment, said longitudinal perforations have a length (l) of at least 15 cm and the density of said perforations along the injection well tubing and, optionally, a well casing in the injection well, are chosen depending on the fluid flow rate at the permeable zones.|[0019] According to an example not forming part of the present invention, said perforations are radially separated with a gap (R) of at least 15 cm in the well casing.|[0020] According to an embodiment of the first aspect, said renewable energy source is selected from the group consisting of solar energy, wind energy, biofuel energy, hydroelectric power, geothermal energy and other green energy sources.|[0021] According to an embodiment, said method further comprises recycling water recycled back to a storage tank.|[0022] According to another embodiment, during the injecting, a high-pressure zone is created within said injection well below a packed off interval and a low-pressure zone is created during the recycling through the observation well.|[0023] According to yet another embodiment, most of the carbon dioxide and water mixture flows from a high- to a low-pressure zone and most of the fluid volume of the water is recycled back through the observation well. According to an example, at least 50 % of the injected water is recycled, more preferably between 80 % and 100 % of the water is recycled.|[0024] A second aspect relates to a system for controlled enhancement of peridotite in situ mineralization, comprising:| an injection well bored in a rock formation and having a non-corrosive well casing;| a non-corrosive injection well tubing disposed in the injection well;| a packer module connected to the injection tubing and disposed in the injection well;| a renewable energy source;| a gas dissolution module connected to the renewable energy source, wherein the gas dissolution module includes a carbon dioxide and water mixture ejection port, and| wherein all steps are powered by a renewable energy source.|[0025] According to an embodiment of the above second aspect, said packer module is an inflatable unit for hydraulic isolation of an injection interval at a predetermined depth in the injection well.|[0026] According to an example not forming part of the present invention, the packer module is configured to be inflated one or more of an aqueous solution and a gas.|[0027] According to yet another embodiment, the system further comprises:| a packer having a minimum 1 m sealing length;| an on-surface packer controller;| in-line hydrostatic pressure sensors at an upstream end and a downstream end of said packer;| an in-line pressure sensor;| an injection and pumping head units; and| channels for wiring, data acquisition and live monitoring.|[0028] According to another embodiment of the second aspect, the renewable energy source is a hybrid energy source selected from the group consisting of a solar energy module; a renewable energy storage module; a wind turbine; a source of hydroelectric power; a biofuel generator; and other renewable energy sources.|[0029] According to yet another embodiment, said renewable energy source comprises one or more of: a solar photovoltaic panel; a solar inverter; a synchronized biofuel generator; an energy storage module; and control panels and switch gears.|[0030] According to yet another embodiment, said renewable energy source provides power to on-surface and sub-surface modules.|[0031] According to yet another embodiment, the gas dissolution module is installed on the surface for gas transfer of carbon dioxide into water prior to the injection well tubing.|[0032] According to yet another embodiment, said gas dissolution module is configured to inject at a gas flow rate of a minimum of 15 litre per minute, a gas pressure of a minimum 8 bar, and a minimum temperature of 20°C.|[0033] According to an example not forming part of the present invention, said gas dissolution module is configured to inject gas bubbles into a water flow in the well injection tubing of a size less than 100 micrometers into a water flow in the non-corrosive well injection tubing.|[0034] According to yet another example not forming part of the present invention, said well casing is about 18 to 23 cm (7 to 9 inches) in diameter.|[0035] According to another example not forming part of the present invention, said well casing comprises longitudinal perforations of a length (l) of at least 15 cm.|[0036] Preferably said perforations are longitudinally separated with a gap (L) of at least 30 cm. These perforations and their spacing is schematically illustrated in Fig. 11, which shows a longitudinal section of a well casing (A), as well as a cross section (B) of the same, indicating the length (l), and the longitudinal (L) and radial (R) spacing of the cut-outs.|[0037] As previously mentioned, peridotite rocks contain two types of silicate minerals: olivine and pyroxene. Olivine rocks often contain magnesium, oxygen, and silicon. Olivine is the most abundant mineral in the earth's mantle until a depth of 700 km. The composition is usually a combination of SiO4 and Mg2+. Typically, silicon bonds with 4 oxygen molecules forming a pyramid structure so that the charges of cations and anions are balanced, and Mg2+ occupies the empty space between the SiO4 structure. These bonds can be easily triggered to react with carbonic acid. The reaction of olivine with CO2 can be accomplished by the following reaction pathway:|        MgSiO4 + 2 CO2 → 2 MgCO3 + SiO2     [1]|[0038] It is also proven that the rate of reaction increases significantly by introducing water. Water helps CO2 to be solubilized forming carbonic acid and therefore making the mineralization and ion exchange process far easier and more efficient. Below is the reaction pathway in presence of water:|        CO2 + H2O → H2CO3 → H+ + HCO3-     [2]|        Mg2SiO4 + 4 H+ → Mg2+ + SiO2 + 2 H2O     [3]|        Mg2+ + HCO3- → MgCO3 + H+     [4]|[0039] Peridotite contains mainly the mineral's olivine and pyroxene. In the presence of water and CO2, the following reaction occurs:|        Mg2SiO4 (olivine) + CaMgSi2O6 (pyroxene) + 2CO2 + 2H2O -> Mg3Si2O5(OH)4 (serpentine) + CaCO3 (calcite) + MgCO3 (magnesite)|[0040] The present disclosure relates to a method that utilizes the above reaction pathways (especially equations 2 - 6) to convert and/or store CO2 into peridotite rocks, as defined above, as a first aspect of the invention. The proposed method also enhances the above reaction rates leading to complete mineralization of total injected CO2 volumes within two to twelve months from injection. The invention also discloses various operating conditions such as temperature, pressure, flowrate (depends on rock permeability), etc. that affect the process efficiency, and at which improved sequestration is obtained. Some embodiments of the present invention also cover engineering aspects such as utilizing renewable energy, water looping, and process configuration and design.|[0041] Another aspect not forming part of the present invention concerns a method for carbon dioxide sequestration utilizing pyroxene minerals. Pyroxene is one of the groups in an inosilicate mineral, which is also abundantly found out in peridotite. The general chemical formula for pyroxene is AB(Si)2O6, in which A can be a cation such as sodium (Na+), calcium (Ca2+), manganese (Mn2+), iron (Fe2+), magnesium (Mg2+), and lithium (Li+), and B is calcium (Ca), sodium (Na), iron (Fell) or zinc (Zn), manganese (Mn) or lithium (Li) and B is manganese (Mn2+), iron (Fe2+, Fe3+), magnesium (Mg2+), aluminum (Al3+), chromium (Cr3+), titanium (Ti4+). Most commonly, pyroxene can often be found as CaMg(SiO3)2. Naturally, pyroxene reacts with CO2 according to the following equation:|        CaMF(SiO3)2 + 2 CO2 -> CaMg(CaCO3)2 + 2 SiO2     [5]|[0042] However, similar to olivine, water increases the rate of reaction, therefore, in presence of water, below is the reaction pathway for CO2-pyroxene reaction:|        CaMgSiO6 + CO2 + H2O -> Ca2Mg5Si8O22(OH)2 + CaCO3 + SiO2     [6]|BRIEF DESCRIPTION OF THE DRAWINGS|[0043] The drawings show embodiments of the disclosed subject matter for the purpose illustrating the invention. However, it should be understood that the present application is not limited to the precise arrangements and instrumentalities shown in the drawings, wherein:| FIG. 1 is a schematic process flow diagram of a system and method according to some embodiments of the disclosed subject matter;| FIG. 2 is schematic process flow diagram of a system and method according to some embodiments of the disclosed subject matter;| FIG. 3 is schematic process flow diagram of a system and method according to some embodiments of the disclosed subject matter;| FIG. 4 illustrates a renewable energy module according to some embodiments of the disclosed subject matter; and| FIG. 5 is a diagram of a well log data that reports level of porosity of rock formation.| FIG. 6 shows two diagrams, unprocessed and processed pressure and flow rate data of a system and method according to some embodiments of the disclosed subject matter;| FIG. 7 is diagram showing the packer pressure of a system and method according to some embodiments of the disclosed subject matter;| FIG. 8 is diagram showing water quality monitoring results (alkalinity, total dissolved solids (TDS), electrical conductivity (EC), and pH) recorded during a five-day test run operating a system and method according to an embodiment of the disclosed subject matter;| FIG. 9 shows the pressure and flow rate during a five-day test run of a system and method according to an embodiment of the disclosed subject matter;| FIG. 10 schematically shows an embodiment which corresponds to the set-up used in the example.| Fig. 11 shows a longitudinal section of a well casing (A), as well as a cross section (B), indicating the length (l), and the longitudinal (L) and radial (R) spacing of the perforations.|DETAILED DESCRIPTION|[0044] Referring now to FIG. 1, the embodiments described include systems and methods for sequestering carbon dioxide via in situ carbonation of peridotite. The system illustrates a carbon capture module (B), a system for accelerated in situ CO2 mineralization (A), comprising an injection module (110), feeding CO2 through a bore hole into a peridotite rock formation (P) where the process of mineralization takes place (M), a recovery system and a monitoring module (120), said system being powered by renewable energy from an energy generating and/or storage module (C), for example solar panels or generators operating on biofuel, to mention two non-limiting examples. In a direct capture module (B), ambient air (AA) is circulated through a contactor system where the air comes in contact with one or more chemicals capable of reacting with and trapping CO2, for example potassium hydroxide, is concentrated and purified, whereafter the captured CO2 is compressed. The compressed CO2 can be directly fed into the system (A) or stored and transported to an in situ mineralization site (A).|[0045] Referring to FIG. 2, some embodiments of the disclosed invention include a water looping system having a water storage module (210), a carbon dioxide injection module and injection well (220), a peridotite formation here schematically illustrated as a substantially horizontal layer (P), and an observation well module (230) for monitoring and controlling carbonation reactions. The process begins by identifying a suitable location with the peridotite layer being at least 0.5 km thick. An injection borehole is drilled into this peridotite layer. Said borehole should be at least 0.5 km deep and up to a maximum of 1.8 km in depth with the preferred depth being between 0.8 to 1.2 km deep. An observation borehole is drilled alongside the injection borehole with hydraulic connection between the two holes. The injection borehole is fitted with an engineered well casing (preferably steel or concrete) which is perforated at the targeted areas for peridotite mineralization in the geological formation (see FIG 11 and the text further below for more details). In the continuous injection process water is first pumped from the observation borehole or another source to a buffer storage tank on surface. The buffer tank is fitted to receive water from different sources such as underground water resources, sea water, treated water etc. The water, at ambient temperature, is then pumped at pressure through the injection pipeline to the injection borehole well head by using a set of booster pumps. The formation temperature at 1 km depth is about 60 - 80°C. Pumping water to this formation will also help controlling the temperature at the site and, consequently, gives greater control over the reaction rate.|[0046] A preferred embodiment of the invention utilizes water looping to minimize the consumption, loss and/or use of water during the CO2 fixation process (sequestering). The water mass ratio of the amount of water injected into a subterranean geologic formation (e.g., a rock or peridotite formation) and the amount of water that is recovered at the recovery well (e.g., observation borehole, monitoring borehole or return well) is preferably close to 1: 1. Engineering the ingress point at which water injected into the borehole enters into the rock formation and/or engineering of a rock formation that with fissures or fractures functions to improve the overall recovery of water and reduces water loss. Water flow entering the geologic formation from the injection borehole can be directed by careful placement of longitudinal perforations in well tubing present inside the injection borehole or the casing surrounding the borehole in contact with the geologic formation. Preferably the perforations are disposed within a zone of injection that corresponds to a shortest distance direct line from the borehole wall of the injection borehole to the borehole wall of the return well. Perforations in the borehole are disposed in the casing of the borehole in only a single hemisphere of the borehole, e.g., the hemisphere encompassing the shortest distance direct borehole-borehole line. Disposing the perforations in this way functions to reduce unwanted or unintended flow of water in a direction away from the recovery well. Alignment of the perforations with fractures and fissures that are in hydraulic communication with the recovery well may also be favored.|[0047] The longitudinal perforations preferably occur at depths in the injection borehole that are within the target zone of the geological formation proximal to an upper boundary. Additional perforations at progressively deeper borehole depths, but preferably in the same hemisphere, may extend downwardly into the borehole proximal to a maximum depth of the peridotite-containing rock formation. The recovery borehole preferably has a depth that is at least the same as the maximum depth of the perforations of the injection borehole. In other embodiments the recovery borehole has a depth that is deeper than the deepest perforation of the injection borehole such that water flowing by gravity will pool or collect at the deeper portions of the recovery borehole and thereby minimize water loss. Preferably the recovery borehole depth is no greater than the maximum depth of the rock formation that comprises mainly peridotite.|[0048] Total dissolved solids of the water may decrease as the water passes through the rock formation. In this manner the recovery borehole collects water that is of greater purity the water (CO2 rich fluid-mixture) initially injected into the injection borehole. Saline water, brackish water and/or seawater can have a reduced total solids content after flowing through the injection borehole, through the rock formation and recovery borehole.|[0049] Water looping is likewise utilized in above ground handling and treatment of water, e.g., during processing of water collected in the recovery borehole prior to injection into the injection borehole. Preferably at least a majority of the water injected into the injection borehole is recycled or reused for later injection of additional CO2 into the injection borehole. Preferably, all of the water obtained from the recovery borehole is used in the injection borehole after the addition of further CO2. Water looping in this manner minimizes the need to pre-purify water prior to injecting into the rock formation and maximizes the reuse and recycle of the water.|[0050] The recovery borehole is preferably an uncased well so that water may more easily enter and collect in the recovering borehole. In other embodiments the recovery borehole is partially cased with at least a major portion of the borehole length that passes through the target zone remaining uncased. Partial casing of the recovery borehole reduces loss of water in strata above and/or below the target zone that may be porous and/or otherwise hydraulically communicate with other underground rock formations that do not permit recovery of water.|[0051] In a preferred embodiment of the invention the CO2 rich fluid-mixture is injected into the geologic formation through the injection borehole at an ambient temperature preferably 25-30° C ±15°C, preferably ±10°C, more preferably ±5°C. As recognized by one of skill in the art, cooler temperatures are capable of dissolving greater amounts of CO2. This aspect of the invention is particularly well-suited for evaporative cooling of the return fluid obtained from the recovery, observation or monitoring well.|[0052] Fixation of the CO2 in the CO2 rich fluid-mixture injected into the geologic formation is, in a preferred embodiment, essentially complete. For example, a CO2 rich fluid-mixture injected into the injection borehole forms a return fluid collected at the return well (observation or monitoring borehole) having an amount of dissolved CO2 that is less than 0.1 wt-%, preferably less than 0.05 wt-%, more preferably less than 0.01% by weight based on the total weight of the return fluid and the CO2. The return fluid may be completely free of CO2.|[0053] In a still further embodiment of the invention the geologic formation is first subject to pretreatment with water or an aqueous solution before the CO2 rich fluid-mixture is injected therein. Pretreatment with water or aqueous solution can enhance initial absorption and fixation of CO2. Treatment with an aqueous solution such as an aqueous acidic solution may enhance CO2 absorption of fixation by forming voids and crevices within the geologic formation thereby providing enhanced fluid flow through the formation and/or otherwise activating the peridotite formation for reaction with CO2.|[0054] Prior mechanical fracturing of the geologic formation is not required. Preferably the CO2 rich fluid-mixture is injected into the geologic formation at pressures substantially less than those necessary in order to mechanically fracture the formation.|[0055] CO2 is dissolved in fluid on surface through a gas dissolution module into the pressurized water stream between the booster pumps and the injection well head. Artificial conservative tracer(s) are used to trace the injected CO2-saturate fluid within the storage reservoir utilizing the monitoring / observation boreholes. Molar ratio of tracers to CO2 are kept constant at the injection well, whereas changes of this ratio in the observation borehole indicates CO2 abatement via reaction with peridotite. The CO2 gas is dissolved once it mixes with the pressurized water stream, where it is carried to the target injection zone. The gas pressure in the pressurized water stream is set to be below or close to the hydrostatic pressure at the target injection depth. The CO2 rich fluid-mixture is then injected through the injection borehole well head. The injection well head is connected through a non-corrosive pipe to a packer system (312) that is installed just above the target injection zone. The packer system (312) hydraulically isolates the column for injection of CO2 rich fluid-mixture into the peridotite rock formation. The injected CO2 rich fluid-mixture is dispersed through the annulus within the peridotite formation where the dissolved CO2 reacts in-situ with the peridotite rocks. The dispersion of the CO2-rich fluid mixture happens via perforated well casing which targets a specific pre-determined permeable layer of the peridotite. Monitoring of both the injected CO2 rich fluid-mixture on surface and the hydraulic pressures at the injection interval is continuously logged for analysis using sensors and a data acquisition system. Samples from the injection borehole below the packed off interval are collected through a membrane system to the surface for continuous dissolved CO2 analysis. The injection well head is fitted with CO2 gas detection devices to monitor any potential leakages of the gas on the surface. This whole process is advantageously powered by a hybrid-renewable system to keep a carbon footprint low and maximize the net amount of CO2 eliminated (see section 2 below).|[0056] The CO2 rich fluid-mixture is preferably injected into the borehole within the target zone by delivery through a steel or polymer tubing string. In this embodiment contact between the borehole wall and/or casing with the CO2 rich fluid-mixture is minimized except for at a location where the borehole is perforated within the target zone of peridotite. The point at which the CO2 rich fluid-mixture is released from the tubing string into the borehole can be determined by using packers at different depths or different positions within the borehole. Preferably packers are set both upstream and downstream of the injection point(s) within the injection borehole at which the CO2 rich fluid-mixture is released from the tubing string into the borehole and through perforations in the borehole casing into the rock formation. Preferably a packer is set above the maximum depth of the target formation and below the minimum depth of the target formation to limit the release of the CO2 rich fluid-mixture into the portion of the borehole which directly corresponds with and is encompassed by a peridotite rock formation.|[0057] In a preferred embodiment of the invention the return fluid formed when the CO2 rich fluid-mixture (e.g., CO2 saturated water) passes through the geologic formation (e.g., peridotite reservoir) is subject to cooling after return to the surface. In order to make good use of renewable resources a portion of the return water is used in an evaporative cooling process. For example, when returning to the surface the return fluid may flow through a manifold system in which the return fluid is divided into at least two portions. A main portion is piped to another location, for example, to a storage tank or directly to the well injection point for further mixing with CO2 and later injection into the injection borehole. The second, typically smaller, portion is transferred to an evaporative cooling apparatus and evaporated. A return fluid pipe used for transferring the main portion of the return fluid may disposed in a second pipe of larger diameter forming an annulus space between the outer surface of the return fluid pipe and the inner surface of the second pipe. The second portion of the return water may then be sprayed or passed into the annulus in the presence of a stream of gas in which the second portion of the return fluid evaporates thereby providing cooling effect to cool the fluid in the return fluid pipe. Preferably, the gas flow used in the evaporative cooling is CO2 which may subsequently be transferred to a CO2 storage facility and/or the well injection point for injection into the geological formation. The gas stream exiting the annulus includes evaporated water and mainly carbon dioxide gas.|[0058] Injection of the CO2 rich fluid-mixture into the injection well may be under conditions permitting effervescence of CO2 from the CO2 rich fluid-mixture. The formation of bubbles in the geologic formation may permit enhanced absorption and/or fixation through effects that include, for example, disruption of water flow as a two-phase mixture and collisions of CO2 bubbles with features of the geologic formation surface.|[0059] The hybrid-renewable system preferably includes a plurality of photovoltaic (PV) cells to generate electricity from sunlight. Electrical storage facilities are typically included. PV panels are preferably mounted over the injection system and over storage tanks. Especially with respect to mounting above the injection system, electrical energy obtained from the PV cells may be used directly thereby avoiding the complexities and expense of long electrical transfer lines.|[0060] Aspects of the invention include portability of injection and renewable energy components. Portability, especially as it relates to the injection system, is especially advantageous for relocation of the injection equipment and energy generating equipment to new locations of geologic material. As a geologic formation of peridotite becomes reacted/saturated with CO2, the efficiency of further CO2 fixation decreases. It is then advantageous to seal the return fluid well (for example by cementing) and relocate injection of the CO2 rich fluid-mixture to an injection point located differently than an initial well.|[0061] Referring to FIGs. 2 and 3, some embodiments of the disclosed subject matter include a continuous injection method and other embodiments show an overview of the CO2 injection system. A submersible pump (SP2) is installed in the observation borehole at depth and is used to pump ground water into an on-surface storage tank (340). SP2 flow rates and pressures preferably match the permeability of the subsurface formation. The on-surface storage tank (340) is equipped with sensors that automate the operation of the SP2 and acts as a buffer between the observation and injection boreholes. In one embodiment, the tank has a volume of at least 5000 L. The on-surface storage tank is also fitted with coupling connections to receive water from different other sources. A set of booster pumps (BP1, BP2) are used in parallel to inject water from the on-surface storage tank (340) at pressure to the injection well (320). The flow rates of the fluid-mixture are adapted to the permeability of the target injection zone at the injection borehole. A permeability test is carried out to determine these rates at the injection borehole prior to injecting CO2 rich fluid-mixture. One or more dosing pumps (DP) is/are used to regulate the flow of a tracer fluid from a tracer tank (360). In one embodiment, said tank has a volume of at least 100 l, and fluorescein is used as the tracer.|[0062] The tracer is injected into the water stream at pressure, in the pipe section between the BPs and the injection well head, using a set of dosing pumps (DPs). The dosing rate is regulated throughout the injection process. The tracer fluid is used to trace the injected CO2 rich fluid-mixture in the subsurface using observation boreholes (333). A gas dissolution module (310) is installed on a flanged pipe section, before the injection well head. CO2 gas is injected at pressure into the water stream. CO2 gas injection pressure is regulated by a mass flow controller device that is connected to a gas manifold. The gas manifold controls the supply of CO2 gas from the CO2 storage tanks at a regulated pressure level. The gas dissolution module is designed to maximize gas transfer efficiencies as well as buffer capacities within the injection pipe column and to release CO2 gas bubbles at <50 µm to maximize bubbles surface area for solubility and to reduce the buoyancy effect. The CO2 rich fluid-mixture is injected into the subsurface through an injection well head on the injection borehole. The injection well head holds the string assembly that is suspended on a supported mechanical system on the surface. The string assembly is composed of (1) Non-corrosive fluid pipes that connect the injection well head on surface to the packer system (312) and acts as the injection column for the CO2 rich fluid-mixture; (2) Submersible pump (SP1) placed on the injection borehole and connected on the string assembly used to pump back the injected CO2 rich fluid-mixture any at given point during the injection process; (3) Shut-In-Tool (SIT, 311) that is used to isolate the injection interval once the CO2 rich fluid-mixture is injected into peridotite formation which acts as a safety measure to prevent any undissolved CO2 gas bubbles from rising back to the surface during any maintenance operations; and (4) packer system or packer module (PS) consists of a water or gas inflation packer that is used to pack off the interval at the target injection zones. The packer is equipped with various sensors to monitor hydraulic pressures of the column above and below the packed off interval as well as the packer pressure. The PS is also set-up with other sensors for live monitoring of the injection zone interval. The interval is packed off at a differential to the column hydrostatic pressure ensuring a proper seal is maintained once hydraulic pressure below the packed off interval begins to increase.|[0063] In addition to conventional tracers, confirmation that CO2 injected into the geological formation is absorbed and fixed can be determining by measuring the CO2/fluid ratio at the well injection point in comparison to the CO2/fluid ratio in the return fluid at a surface return site. The CO2 injected into the geologic formation can be modified to include an amount of nucleotide-labeled material (for example CO2 labeled with 17O or CO2 labeled with 14C) and compared with a corresponding amount (concentration) in the return fluid.|[0064] A fluid recovery well (330) for the return fluid can be located at a distance from the CO2 injection well (320) such that the distance the CO2 rich fluid mixture traverses through the geologic formation is sufficient to absorb and/or fixate substantially all of CO2 in the CO2 rich fluid-mixture. This distance may vary depending on the location of the injection well, the structure of the geologic formation and the availability of water for injecting the CO2 rich fluid-mixture into the geologic formation. A distance of 0.1-10 km, preferably 0.2-5 km, 0.5-1 km or 0.7-0.9 km can be used.|[0065] Referring to FIG. 4, some embodiments of the disclosed subject matter include a renewable energy system that consists of for example, a solar cell module (410), solar inverters (420), an energy storage module comprising a battery system (460), an energy management system, EMS (470), wind turbines (not shown), and a biofuel module, comprising for example synchronized generators (440), a fuel tank (450) for holding biofuel. Further, switchgear (430) and an energy meter (480) is preferably included. The renewable energy system works in such a way that during daytime, solar energy is used to supply the loads to all injection systems on the ground. Excess renewable energy is stored to be used for improved system performance and for operation during night-time. During night-time operation, energy stored is used for supplying the required loads. Based on site consumption, the energy stored would be utilized to supply the night loads throughout the entire night period along with renewable energy sources that can operate at night (Eg; wind turbines and biofuel generators). There is no loss in power while transitioning from solar/off-grid operation to energy storage, the stored energy will instantly take over supply and smoothly transition to energy storage operation only. The hybrid controller will be responsible for communication among the inverters, storage, biofuel generators and the overall transfer of power within the system|[0066] Another preferred embodiment of the present invention is the injection borehole (310, 320) development. This involves increasing wellbore diameter from 16.5 cm to 25 cm for the full depth of the borehole and permanent installation of non-corrosive casing, ideally 7-inch (17.78 cm) in diameter, with slotted sections or screen in the injection zone. Drilling Rate of Penetration (ROP) can be used to interpret rock properties. A slower rate of penetration indicates a requirement for higher fracture stress by the drill bit to break the rock. For rock types that are known to be homogenous this information will serve as an indication for the level of porosity at different depths. Porosity reduces the fracture stress of bulk rock type and therefore increased ROP is indicative to higher porosity.|[0067] Referring to FIG. 5, this confirms that faster ROP above 100 meters below ground level (mbgl) is indicative of a higher level of porosity and therefore a higher water to rock ratio. Below 100 mbgl the porosity is lower and therefore the water to rock ratio is expected to be lower. However, the plot shows distinct regions below 100 mbgl where the ROP increases which indicate the presence of intervals with higher porosity.|[0068] In another preferred embodiment of the present invention, downhole injection assembly system is described. A packer tool (312) is installed to isolate the injection interval from the remaining part of the borehole. This allows for installation of pressure monitoring devices above and below the packer tool (312). A shut-in tool (311) is installed to isolate the injection interval after injection to ensure no upward drift of injected fluid to the top intervals. The submersible pump (SP-1) is used to draw water from the isolated injection interval and for sampling purposes. Downhole injection piping and equipment are pressure rated to withstand injection pressures required. Well head installed constitutes of two ports: 1) Incoming injection fluid and 2) outgoing sampling port. It is noteworthy to mention that a check should carried out for any blockages and remove any existing blockages for the complete depth of the open borehole. A submersible intake pump (SP2) is used in the observation well (333). A submersible pump is used to draw water from the observation well to be used for injection purposes in the injection borehole. The submersible pump is placed at least 60 mbgl to draw water from above the injection interval in injection borehole. This is done to minimize interference in the event of existing subsurface connectivity between the two wellbores. The submersible pump is sized on the following flow basis: provide a flow rate of a minimum of 0.1 L/s and a minimum of 8640 L/day under the recommended operating schedule. The submersible pump is sized on the following pressure basis: placement depth is a minimum of 60 mbgl (meters below ground level); pumping head must be sufficient to deliver water to surface at ease. Submersible pumps cannot operate continuously for extended period. Therefore, the observation well water will be supplied with temporarily stored water in a buffer tank to counteract the intermittent nature of submersible pumps.|[0069] In another preferred embodiment of the present invention a water buffer tank is described. The water buffer tank or tanks will hold water from observation wells or from another source to counteract pumping intermittency, flow intermittency, stabilize pressure and for additional process control and operational reasons. Sizing of the buffer tank is dependent on the selection of the submersible pump and is made on the following basis: 1) the tank holds sufficient capacity to allow the submersible pump to deliver the daily required volumes following the recommended hours of operation schedule; and 2) the tank should hold sufficient capacity to allow for continuous and uninterrupted draw of at least 0.1 L/s for injection. In a test run performed by the present inventors, a buffer tank capacity of 5500 L was chosen.|[0070] The buffer tank also plays a critical role of dampening pressure fluctuation caused by natural changes in water levels in the observation borehole and will therefore allow for a stable pressure supply by the injection pumps. The injection pump/s are selected for continuous and uninterrupted operation. The sizing of the pumps are made on the following basis: 1) flow rate set at a minimum of 0.1 L/s; 2) sufficient overpressure to cover hydrostatic head at the injection interval, major and minor head losses due to the system assembly, and account for pressure build up to allow flow through the injection zone is done through energy balance equation used to calculate head loss in system and Darcy's law used to determine flow into the injection zone by assuming linear cylindrical outward flow; and 3) provide a pressure high enough to ensure solubility of dissolved CO2 on surface at steady state flow conditions. A dosing pump (DP1) is used to inject set volume (at least 5 mL/min) of liquid conservative tracers, e.g. fluorescein, into along with the injection fluid. Dosing is done inline after the injection pumps / booster pumps. Due to the dynamic changes in the subsurface pressure conditions after the start of injection flow rate is expected to change over time to reflect the change in conditions. The water flowmeter will record changes in the injected fluid flow rate over injection time to monitor the system behavior with respect to subsurface pressure and to allow for accurate accounting of total injected volumes and to assist with dynamic data interpretation. Preferably, an electromagnetic flow meter is selected for its uniform behavior, responsive reading time, un-interruption to flow and due to the homogenous nature of the injected fluid that allows for consistent magnetic behavior and therefore consistent flow reading accuracy. The flow meter is calibrated specifically for the project application to ensure the accuracy of the meter for the expected flow conditions.|[0071] Another preferred embodiment of the present invention is a CO2 injection system development. The Automatic CO2 gas switchover manifold is used to stabilize and regulate the pressure from CO2 tanks. CO2 tank pressure gradually decreases as the contained gas is depleted and due to the sensitive thermodynamic behavior of gas temperature swings between day and night has a significant impact on tank supply pressure. Further the expansion of the gas through various valves and through the pipes also associate with temperature changes and consequently pressure changes. To allow for accurate and controlled pressure delivery the manifold regulates the delivery pressure from tanks to a selected setpoint. The manifold also ensures uninterrupted CO2 supply by operating one wing (301) and keeping the second wing (302) on standby. Once the delivery pressure from the primary wing is not capable of meeting the target setpoint the manifold automatically switches to the secondary standby wing. Gas flow is difficult to regulate due to the impact of temperature upstream and downstream pressure on the flow rate. The gas flow controller will adjust the flow to account for all gas flow fluctuation to maintain a stable flow rate of a minimum of 1.3 g/s. A gas dissolution module is used to mix CO2 into the water.|[0072] A gas dissolution system (310) can be used to maximize the gas liquid contact surface area to minimize gas dissolution time and to ensure complete dissolution of CO2 in the injected water. This system is placed after the injection pump as higher pressures promote higher gas solubility. The system is designed to dissolve gas with a bubble diameter less than 100 µm and is specifically designed and tuned for the project application accounting for both water and gas flow rates and pressures. The design of the system also accounts for the gas pressure drop across the system to balance with the maximum delivery pressure available from the manifold and additional pressure drops in the gas delivery system, to ensure flow into the high-pressure water line. The housing of the system is designed to accommodate all components with minimal interruption to water flow, provides easy internal access for servicing purposes and allows for slower flow velocity so that the dissolution residence time matches the fluid residence time in the unit.|[0073] In another preferred embodiment include a monitoring system. Monitoring includes a complete water quality testing, pH, total dissolved solids (TDS), electrical conductivity (EC), temperature, Oxidation Reduction Potential (ORP) and other physical properties. A sample from borehole water has been collected after drilling activity for complete water quality testing by an independent laboratory. A submersible pump placed at a minimum of 60 mbgl was used to collect water for pH, EC, TDS, Temperature and ORP on site. An additional submersible pump was placed at a minimum of 60 mbgl used to collect samples to test for cations, anions, alkalinity, and dissolved CO2. In addition, monitoring system also included the injected conservative tracers to monitor the change of the molar ratio of CO2 to tracers, which was kept constant in the injection well. Changes in this ratio will indicate CO2-water-rock reactions and thus CO2 abatement. In addition, utilizing natural tracers such as stable carbon, strontium, magnesium and calcium isotopes, it is possible to determine the reactivity of the peridotite system to mineralize the injected CO2.|[0074] In another preferred embodiment of the present invention, the fluid flow path between the injected borehole and the observation borehole are natural fractures that extend in other directions than upward or downward or in case of limiting natural fractures, a fracture network that has been induced through permeability enhancement.|EXAMPLE|[0075] In a pilot scale experiment carried out in the Samail Ophiolites in the Sultanate of Oman and supervised by the inventors, a system was constructed as schematically shown in FIGs 3 and 10. Two boreholes (1020, and 1030) were drilled into the rock until a peridotite layer (P) was reached. The first borehole (1020) was fitted with well casing which was perforated (See FIG 11) at the targeted areas for peridotite mineralization. A packer (1012) was used to isolate the peridotite layer (P) for targeted injection of the CO2 - water mixture. A submersible pump (SP1) located in the borehole (1020) above the packer was used to recoup the injected fluid mixture after an incubation period for sampling and analysis, to prove occurrence of mineralization (M). A submersible pump (SP2), in the opposite borehole (1030), was used to pump groundwater for injection into the injection borehole.|[0076] CO2 was fully dissolved in the groundwater on the surface using a gas dissolution module (310) at a pre-defined CO2 to water ratio. A conservative tracer (here sodium fluorescein) was metered into the water injection stream using a dosing pump, operated at a specific rate that accounted for dilution in the subsurface. The CO2 saturated fluid was injected via a non-corrosive pipe to the hydraulically isolated target injection interval in the first borehole (1020). A monitoring borehole (not shown) that was hydraulically connected to the injection borehole via a natural fracture network in the peridotite reservoir, was utilized for estimating the CO2 mineralization capacity of said reservoir rock. Samples were also taken in the first borehole (1020) in an upper section above the packer (1012) peridotite layer (P).|[0077] A monitoring equipment was used to monitor the degree of CO2 abatement via peridotite-water reactions, utilizing the molar ratio of CO2 to said conservative tracer. Using the measured concentration of said conservative tracer in the injected fluid and the fluid retrieved in the monitoring borehole allowed calculating the dilution of the injected fluid with ambient reservoir groundwater via dispersion. Changes in the conservative tracer to CO2 molar ratio from the injection borehole (which is fixed for said injection) to the observation borehole indicated CO2-peridotite reactions and thus a loss of CO2 along the said flow path. CO2 mineralization could be quantified by monitoring the dissolved CO2 content in the injected fluid and in the observation borehole via said membrane system. Decreased dissolved CO2 concentration in the observation borehole fluids compared to the initial concentration in the injection borehole clearly indicated that an amount of CO2 was sequestered.|[0078] The experiment was performed during a period of six days, and the measured results are shown in FIGs 5 - 9. The results indicated that the system remained stable and operational during the test period. (EP4134513)|TECHNICAL FIELD|[0001] The present disclosure relates to a system and method for permanent carbon dioxide (CO2) sequestration in peridotite rock formations. More specifically, the present disclosure relates to accelerating and controlling natural peridotite carbonation between peridotite and a source of carbon dioxide to be sequestered. The present disclosure also relates to methods for permanently sequestering carbon dioxide that is captured from industrial emissions, atmospheric air, or that contained in bodies of fluid. The present disclosure also relates to the use of renewable sources of energy for carbon capture plants and carbon storage process equipment.|BACKGROUND|[0002] Over the past century, industrial activities, particularly fossil fuel consumption, have caused a dramatic increase of the CO2 concentration in the atmosphere. This anthropogenic impact on the global carbon cycle is the main reason for the observed climate change over the past decades. Global climate change has been linked to various other phenomena, including hurricanes, droughts, floods, glacier retreat, and rising sea levels. A recent United Nations Environment Programme report on global warming indicates that `human influences will continue to change atmospheric composition throughout the 21st century' and carbon dioxide makes the largest contribution out of these human activities. CO2 is released into the atmosphere by the combustion of fossil fuels such as coal, oil or natural gas, and renewable fuels like biomass; by the burning of, for example, forests during land clearance; and from certain industrial and resource extraction processes. As a result, `emissions of CO2 due to fossil fuel burning are virtually certain to be the dominant influence on the trends in atmospheric CO2 concentration during the 21st century' and 'global average temperatures and sea level are projected to rise'.|[0003] As such, large efforts have been made to develop effective carbon capture and storage (CCS) methods that remove CO2 from the atmosphere. Chemical weathering is a slow process that controls atmospheric CO2 concentrations over geological time scales. Several prior art references have proposed accelerating chemical weathering to counter global climate change. The goal of enhanced weathering is to hasten silicate mineral weathering rates to accelerate the removal of CO2 from the atmosphere in the form of dissolved inorganic carbon and/or as carbonate minerals. Because of their relatively rapid dissolution rates, enhanced weathering has focused on mafic and ultramafic rocks.|[0004] Because of its high concentration of Mg, tectonically exposed peridotite from the Earth's upper mantle, which is composed largely of the mineral olivine ((Mg, Fe)SiO4), with lesser proportions of pyroxene minerals ((Mg, Fe, Ca)Si2O) and spinel ((Mg, Fe)(Cr, Al)O), and its hydrous alteration product serpentine (Mg3Si2O5(OH)5), have been considered a promising reactant for conversion of atmospheric carbon dioxide to solid carbonate. Natural carbonation of peridotite has been found to be surprisingly rapid compared to other types of rocks. For example, carbonate veins in mantle peridotite in Oman have an average age of approximately 26,000 years and are not 30 to 95 million years old as previously believed. These data and reconnaissance mappings show that approximately 104 to 105 tons per year of atmospheric carbon dioxide are converted to solid carbonate minerals via peridotite weathering in Oman (Peter B. Kelemen and Jürg Matter, In situ carbonation of peridotite for CO2 storage, PNAS November 11, 2008 105 (45) 17295-17300).|[0005] Mantle peridotite is ordinarily more than 6 km below the seafloor and is strongly out of equilibrium with air and water at the Earth's surface. Its exposure along large thrust faults and along tectonic plate boundaries creates a large reservoir of chemical potential energy. Despite the available chemical potential, engineering techniques for carbon sequestration have many challenges. Engineering solutions involve grinding peridotite to a fine powder, purifying carbon dioxide gas, using reaction vessels at elevated pressure, and/or heating reactants to 100 degrees Celsius or more, and this comes at a substantial financial and energy cost.|[0006] Various methods have been experimentally evaluated, including direct carbonation of olivine and serpentine powders at elevated temperature, dissolution of serpentine or olivine in hydrochloric acid followed by carbonation of Mg and cations in solution, and reaction of olivine and serpentine with carbonic acid (very similar to natural alteration). Reaction kinetics have been found to be too slow for significant sequestration of carbon dioxide unless the olivine or serpentine reactants are raised to more than 100 degrees Celsius, ground to a fine powder, and/or pre-treated at above 600 degrees Celsius to increase reactive surface area. For the most part, because of the requirements for heating and processing, these approaches have been found to be too expensive in financial terms and, more importantly, in energy expenditure, not commercially viable at present.|[0007] US9193594B2 discloses methods and systems for enhancing rates of carbonation of peridotite both in situ and ex situ. In some embodiments, the methods and systems include the following: fracturing a volume of peridotite; heating the volume of peridotite; injecting an adjustable flow of carbon dioxide into the volume of peridotite; injecting bicarbonate materials into the volume of peridotite; and forming carbonate with the volume of peridotite and the carbon dioxide in an exothermic reaction thereby generating a self-sustaining heat source, the heat source heating the volume of peridotite.|[0008] US8524152B2 discloses methods and systems for enhancing rates of in situ carbonation of peridotite. In some embodiments, the methods and systems include the following: fracturing a volume of peridotite in situ; heating the volume of peridotite in situ; injecting carbon dioxide into the volume of peridotite in situ; and forming carbonate in situ with the volume of peridotite and the carbon dioxide.|[0009] US9266061B2 discloses a filter for treating CO2 from a CO2-emitting industrial plant, taking advantage of the fact that peridotite igneous rocks (or material of similar chemical content: basalt, gabbro, dunite, amphibolites, artificially produced Ca, Mg oxides) which are abundant on and close to the Earth's surface, can absorb and contain CO2 gases resultant from industrial activity. This chemical process occurs naturally but has not been utilized to capture high concentrations of CO2 emitted into the atmosphere. Calcium and magnesium oxides of the peridotite react with CO2 to form stable carbonate minerals. The invention enhances and expedites this natural process for the remediation of industrial pollutants such as CO2 from the oil, gas, coal, cement/concrete and like CO2-emitting industries, and provides a resource for materials in construction (concrete), steel, aviation and agricultural and other industries.|[0010] JP2007283279A discloses a global warming suppression technology for decomposing, insolubilizing, and/or purifying soil polluted by hazardous substances and pollutants such as waste products, and the like, suppressing pollutants at the levels or lower than environmental quality standards for soil over long periods, and naturally adsorbing and decomposing carbon dioxide in air via its reaction step during treatment. A pollutant treating agent containing non-calcinated peridotite as a principal component is used for separating and/or decomposing pollutants in addition to perform long-term in solubilization by adding and/or mixing light-burned magnesite, light-burned dolomite, fused phosphate, or calcined shell powder according to types of pollutant. Thus, the polluted area is purified. Furthermore, the agent absorbs a large amount of carbon dioxide in air during the step of using the agent, so that the agent has effects as a low-cost and low-environmental-load-type technique for suppressing global warming.|[0011] CN108658104A discloses a magnesium sinking technique during a kind of peridotite ore production of magnesia, including processing steps such as ore dressing, grinding, purification and impurity removal, flotation processing, magnesium sinking processing, acid leach removal of impurities, flotation purifying, precipitate separation, to increase the purity and recovery rate of magnesia. The method is disclosed to provide a magnesia purity of up to 99.7% or more, and up to 89.7 94.2%.|[0012] PCT/EP2020/064306 (WO/2020/234464) discloses a method and a system of abating carbon dioxide (CO2) and/or hydrogen sulfide (H2S) in a geological reservoir. Water is pumped or transferred from a water source to an injection well. The gasses are merged with the water under conditions where the hydraulic pressure of the water is less than the pressure of CO2 and/or H2S gas at the merging point. The water with CO2 and/or H2S gas bubbles is transferred further downwardly at a certain velocity higher than the upward flow velocity of said CO2 and/or H2S gas bubbles ensuring downward movement of gas bubbles resulting in full dissolution of said CO2 and/or H2S in the water due to elevating pressure. The complete dissolution ensures a lowered pH of the water entering a geological (e.g. geothermal) reservoir which is needed to promote mineral reactions leading to CO2 and H2S abatement. This abatement may be quantified by dissolving a tracer substance in a predetermined molar ratio to said dissolved CO2 and/or H2S and monitored in a monitoring well.|[0013] A process disclosed by D.E.Clark et al. ("CarbFix2: CO2 and H2S mineralization during 3.5 years of continuous injection into basaltic rocks at more than 250°C" by Deidre E. Clark et al., published in Geochimica et Cosmochimica Acta, volume 279, 1 June 2020, pages 45-66) involves the separation of CO2 and H2S from a geothermal exhaust gas stream, dissolution of the separated CO2 and H2S into a condensed waste stream from said geothermal power plant, injection of the gas-charged condensate to a specific depth in the injection well, using a stainless steel pipe installed inside the injection well casing. In addition, effluent water from the geothermal plant is injected into the injection well in order to drag down (wash down) the gas-charged condensate to the target injection depth. There remains a need for improved methods and systems for efficient and practical CO2 mineralization in large scale and with reduced environmental impact.|SUMMARY|[0014] The present disclosure provides an efficient and controlled method for CO2 mineralization into peridotite rocks using renewable energy. Peridotite rocks are known for comprising mostly silicate minerals such as olivine and pyroxene. These types of minerals are active in the presence of solubilized CO2 producing various carbonate rocks. The present disclosure is based on the idea of injecting solubilized carbon dioxide (water-CO2 mixture) into peridotite rock formations and creating efficient reaction pathways by manipulating the operation conditions (temperature and pressure) for the mineralization reaction to happen. Consequently, CO2 be converted into magnesite (MgCO3) and calcite (CaCO3) and stored permanently in the rock formation in mineral form.|[0015] A first aspect relates to a method of carbon dioxide sequestration by in situ mineralization comprising the steps of| dissolving an amount of carbon dioxide into water to form a carbon dioxide and water mixture;| injecting an amount of said carbon dioxide and water mixture into a rock formation comprising peridotite via an injection well, wherein the carbon dioxide and water mixture is flowed through the injection well or an injection well tubing disposed in the rock formation, the injection well and/or injection well tubing having a plurality of longitudinal perforations at a depth of 0.4 to 4 km in the rock formation;| recycling water from said rock formation via an observation well; and| reacting carbon dioxide in said carbon dioxide and water mixture with said rock formation to form calcites and magnesites, and| all steps of the process are powered by a renewable energy source.|[0016] According to an example not forming part of the present invention, said rock formation consists mainly of peridotite.|[0017] According to an embodiment, said injection and observation wells have the same depth.|[0018] According to an embodiment, said longitudinal perforations have a length (l) of at least 15 cm and the density of said perforations along the injection well tubing and, optionally, a well casing in the injection well, are chosen depending on the fluid flow rate at the permeable zones.|[0019] According to an example not forming part of the present invention, said perforations are radially separated with a gap (R) of at least 15 cm in the well casing.|[0020] According to an embodiment of the first aspect, said renewable energy source is selected from the group consisting of solar energy, wind energy, biofuel energy, hydroelectric power, geothermal energy and other green energy sources.|[0021] According to an embodiment, said method further comprises recycling water recycled back to a storage tank.|[0022] According to another embodiment, during the injecting, a high-pressure zone is created within said injection well below a packed off interval and a low-pressure zone is created during the recycling through the observation well.|[0023] According to yet another embodiment, most of the carbon dioxide and water mixture flows from a high- to a low-pressure zone and most of the fluid volume of the water is recycled back through the observation well. According to an example, at least 50 % of the injected water is recycled, more preferably between 80 % and 100 % of the water is recycled.|[0024] A second aspect relates to a system for controlled enhancement of peridotite in situ mineralization, comprising:| an injection well bored in a rock formation and having a non-corrosive well casing;| a non-corrosive injection well tubing disposed in the injection well;| a packer module connected to the injection tubing and disposed in the injection well;| a renewable energy source;| a gas dissolution module connected to the renewable energy source, wherein the gas dissolution module includes a carbon dioxide and water mixture ejection port, and| wherein all steps are powered by a renewable energy source.|[0025] According to an embodiment of the above second aspect, said packer module is an inflatable unit for hydraulic isolation of an injection interval at a predetermined depth in the injection well.|[0026] According to an example not forming part of the present invention, the packer module is configured to be inflated one or more of an aqueous solution and a gas.|[0027] According to yet another embodiment, the system further comprises:| a packer having a minimum 1 m sealing length;| an on-surface packer controller;| in-line hydrostatic pressure sensors at an upstream end and a downstream end of said packer;| an in-line pressure sensor;| an injection and pumping head units; and| channels for wiring, data acquisition and live monitoring.|[0028] According to another embodiment of the second aspect, the renewable energy source is a hybrid energy source selected from the group consisting of a solar energy module; a renewable energy storage module; a wind turbine; a source of hydroelectric power; a biofuel generator; and other renewable energy sources.|[0029] According to yet another embodiment, said renewable energy source comprises one or more of: a solar photovoltaic panel; a solar inverter; a synchronized biofuel generator; an energy storage module; and control panels and switch gears.|[0030] According to yet another embodiment, said renewable energy source provides power to on-surface and sub-surface modules.|[0031] According to yet another embodiment, the gas dissolution module is installed on the surface for gas transfer of carbon dioxide into water prior to the injection well tubing.|[0032] According to yet another embodiment, said gas dissolution module is configured to inject at a gas flow rate of a minimum of 15 litre per minute, a gas pressure of a minimum 8 bar, and a minimum temperature of 20°C.|[0033] According to an example not forming part of the present invention, said gas dissolution module is configured to inject gas bubbles into a water flow in the well injection tubing of a size less than 100 micrometers into a water flow in the non-corrosive well injection tubing.|[0034] According to yet another example not forming part of the present invention, said well casing is about 18 to 23 cm (7 to 9 inches) in diameter.|[0035] According to another example not forming part of the present invention, said well casing comprises longitudinal perforations of a length (l) of at least 15 cm.|[0036] Preferably said perforations are longitudinally separated with a gap (L) of at least 30 cm. These perforations and their spacing is schematically illustrated in Fig. 11, which shows a longitudinal section of a well casing (A), as well as a cross section (B) of the same, indicating the length (l), and the longitudinal (L) and radial (R) spacing of the cut-outs.|[0037] As previously mentioned, peridotite rocks contain two types of silicate minerals: olivine and pyroxene. Olivine rocks often contain magnesium, oxygen, and silicon. Olivine is the most abundant mineral in the earth's mantle until a depth of 700 km. The composition is usually a combination of SiO4 and Mg2+. Typically, silicon bonds with 4 oxygen molecules forming a pyramid structure so that the charges of cations and anions are balanced, and Mg2+ occupies the empty space between the SiO4 structure. These bonds can be easily triggered to react with carbonic acid. The reaction of olivine with CO2 can be accomplished by the following reaction pathway:|        MgSiO4 + 2 CO2 → 2 MgCO3 + SiO2     [1]|[0038] It is also proven that the rate of reaction increases significantly by introducing water. Water helps CO2 to be solubilized forming carbonic acid and therefore making the mineralization and ion exchange process far easier and more efficient. Below is the reaction pathway in presence of water:|        CO2 + H2O → H2CO3 → H+ + HCO3-     [2]|        Mg2SiO4 + 4 H+ → Mg2+ + SiO2 + 2 H2O     [3]|        Mg2+ + HCO3- → MgCO3 + H+     [4]|[0039] Peridotite contains mainly the mineral's olivine and pyroxene. In the presence of water and CO2, the following reaction occurs:|        Mg2SiO4 (olivine) + CaMgSi2O6 (pyroxene) + 2CO2 + 2H2O -> Mg3Si2O5(OH)4 (serpentine) + CaCO3 (calcite) + MgCO3 (magnesite)|[0040] The present disclosure relates to a method that utilizes the above reaction pathways (especially equations 2 - 6) to convert and/or store CO2 into peridotite rocks, as defined above, as a first aspect of the invention. The proposed method also enhances the above reaction rates leading to complete mineralization of total injected CO2 volumes within two to twelve months from injection. The invention also discloses various operating conditions such as temperature, pressure, flowrate (depends on rock permeability), etc. that affect the process efficiency, and at which improved sequestration is obtained. Some embodiments of the present invention also cover engineering aspects such as utilizing renewable energy, water looping, and process configuration and design.|[0041] Another aspect not forming part of the present invention concerns a method for carbon dioxide sequestration utilizing pyroxene minerals. Pyroxene is one of the groups in an inosilicate mineral, which is also abundantly found out in peridotite. The general chemical formula for pyroxene is AB(Si)2O6, in which A can be a cation such as sodium (Na+), calcium (Ca2+), manganese (Mn2+), iron (Fe2+), magnesium (Mg2+), and lithium (Li+), and B is calcium (Ca), sodium (Na), iron (Fell) or zinc (Zn), manganese (Mn) or lithium (Li) and B is manganese (Mn2+), iron (Fe2+, Fe3+), magnesium (Mg2+), aluminum (Al3+), chromium (Cr3+), titanium (Ti4+). Most commonly, pyroxene can often be found as CaMg(SiO3)2. Naturally, pyroxene reacts with CO2 according to the following equation:|        CaMF(SiO3)2 + 2 CO2 -> CaMg(CaCO3)2 + 2 SiO2     [5]|[0042] However, similar to olivine, water increases the rate of reaction, therefore, in presence of water, below is the reaction pathway for CO2-pyroxene reaction:|        CaMgSiO6 + CO2 + H2O -> Ca2Mg5Si8O22(OH)2 + CaCO3 + SiO2     [6]|BRIEF DESCRIPTION OF THE DRAWINGS|[0043] The drawings show embodiments of the disclosed subject matter for the purpose illustrating the invention. However, it should be understood that the present application is not limited to the precise arrangements and instrumentalities shown in the drawings, wherein:| FIG. 1 is a schematic process flow diagram of a system and method according to some embodiments of the disclosed subject matter;| FIG. 2 is schematic process flow diagram of a system and method according to some embodiments of the disclosed subject matter;| FIG. 3 is schematic process flow diagram of a system and method according to some embodiments of the disclosed subject matter;| FIG. 4 illustrates a renewable energy module according to some embodiments of the disclosed subject matter; and| FIG. 5 is a diagram of a well log data that reports level of porosity of rock formation.| FIG. 6 shows two diagrams, unprocessed and processed pressure and flow rate data of a system and method according to some embodiments of the disclosed subject matter;| FIG. 7 is diagram showing the packer pressure of a system and method according to some embodiments of the disclosed subject matter;| FIG. 8 is diagram showing water quality monitoring results (alkalinity, total dissolved solids (TDS), electrical conductivity (EC), and pH) recorded during a five-day test run operating a system and method according to an embodiment of the disclosed subject matter;| FIG. 9 shows the pressure and flow rate during a five-day test run of a system and method according to an embodiment of the disclosed subject matter;| FIG. 10 schematically shows an embodiment which corresponds to the set-up used in the example.| Fig. 11 shows a longitudinal section of a well casing (A), as well as a cross section (B), indicating the length (l), and the longitudinal (L) and radial (R) spacing of the perforations.|DETAILED DESCRIPTION|[0044] Referring now to FIG. 1, the embodiments described include systems and methods for sequestering carbon dioxide via in situ carbonation of peridotite. The system illustrates a carbon capture module (B), a system for accelerated in situ CO2 mineralization (A), comprising an injection module (110), feeding CO2 through a bore hole into a peridotite rock formation (P) where the process of mineralization takes place (M), a recovery system and a monitoring module (120), said system being powered by renewable energy from an energy generating and/or storage module (C), for example solar panels or generators operating on biofuel, to mention two non-limiting examples. In a direct capture module (B), ambient air (AA) is circulated through a contactor system where the air comes in contact with one or more chemicals capable of reacting with and trapping CO2, for example potassium hydroxide, is concentrated and purified, whereafter the captured CO2 is compressed. The compressed CO2 can be directly fed into the system (A) or stored and transported to an in situ mineralization site (A).|[0045] Referring to FIG. 2, some embodiments of the disclosed invention include a water looping system having a water storage module (210), a carbon dioxide injection module and injection well (220), a peridotite formation here schematically illustrated as a substantially horizontal layer (P), and an observation well module (230) for monitoring and controlling carbonation reactions. The process begins by identifying a suitable location with the peridotite layer being at least 0.5 km thick. An injection borehole is drilled into this peridotite layer. Said borehole should be at least 0.5 km deep and up to a maximum of 1.8 km in depth with the preferred depth being between 0.8 to 1.2 km deep. An observation borehole is drilled alongside the injection borehole with hydraulic connection between the two holes. The injection borehole is fitted with an engineered well casing (preferably steel or concrete) which is perforated at the targeted areas for peridotite mineralization in the geological formation (see FIG 11 and the text further below for more details). In the continuous injection process water is first pumped from the observation borehole or another source to a buffer storage tank on surface. The buffer tank is fitted to receive water from different sources such as underground water resources, sea water, treated water etc. The water, at ambient temperature, is then pumped at pressure through the injection pipeline to the injection borehole well head by using a set of booster pumps. The formation temperature at 1 km depth is about 60 - 80°C. Pumping water to this formation will also help controlling the temperature at the site and, consequently, gives greater control over the reaction rate.|[0046] A preferred embodiment of the invention utilizes water looping to minimize the consumption, loss and/or use of water during the CO2 fixation process (sequestering). The water mass ratio of the amount of water injected into a subterranean geologic formation (e.g., a rock or peridotite formation) and the amount of water that is recovered at the recovery well (e.g., observation borehole, monitoring borehole or return well) is preferably close to 1: 1. Engineering the ingress point at which water injected into the borehole enters into the rock formation and/or engineering of a rock formation that with fissures or fractures functions to improve the overall recovery of water and reduces water loss. Water flow entering the geologic formation from the injection borehole can be directed by careful placement of longitudinal perforations in well tubing present inside the injection borehole or the casing surrounding the borehole in contact with the geologic formation. Preferably the perforations are disposed within a zone of injection that corresponds to a shortest distance direct line from the borehole wall of the injection borehole to the borehole wall of the return well. Perforations in the borehole are disposed in the casing of the borehole in only a single hemisphere of the borehole, e.g., the hemisphere encompassing the shortest distance direct borehole-borehole line. Disposing the perforations in this way functions to reduce unwanted or unintended flow of water in a direction away from the recovery well. Alignment of the perforations with fractures and fissures that are in hydraulic communication with the recovery well may also be favored.|[0047] The longitudinal perforations preferably occur at depths in the injection borehole that are within the target zone of the geological formation proximal to an upper boundary. Additional perforations at progressively deeper borehole depths, but preferably in the same hemisphere, may extend downwardly into the borehole proximal to a maximum depth of the peridotite-containing rock formation. The recovery borehole preferably has a depth that is at least the same as the maximum depth of the perforations of the injection borehole. In other embodiments the recovery borehole has a depth that is deeper than the deepest perforation of the injection borehole such that water flowing by gravity will pool or collect at the deeper portions of the recovery borehole and thereby minimize water loss. Preferably the recovery borehole depth is no greater than the maximum depth of the rock formation that comprises mainly peridotite.|[0048] Total dissolved solids of the water may decrease as the water passes through the rock formation. In this manner the recovery borehole collects water that is of greater purity the water (CO2 rich fluid-mixture) initially injected into the injection borehole. Saline water, brackish water and/or seawater can have a reduced total solids content after flowing through the injection borehole, through the rock formation and recovery borehole.|[0049] Water looping is likewise utilized in above ground handling and treatment of water, e.g., during processing of water collected in the recovery borehole prior to injection into the injection borehole. Preferably at least a majority of the water injected into the injection borehole is recycled or reused for later injection of additional CO2 into the injection borehole. Preferably, all of the water obtained from the recovery borehole is used in the injection borehole after the addition of further CO2. Water looping in this manner minimizes the need to pre-purify water prior to injecting into the rock formation and maximizes the reuse and recycle of the water.|[0050] The recovery borehole is preferably an uncased well so that water may more easily enter and collect in the recovering borehole. In other embodiments the recovery borehole is partially cased with at least a major portion of the borehole length that passes through the target zone remaining uncased. Partial casing of the recovery borehole reduces loss of water in strata above and/or below the target zone that may be porous and/or otherwise hydraulically communicate with other underground rock formations that do not permit recovery of water.|[0051] In a preferred embodiment of the invention the CO2 rich fluid-mixture is injected into the geologic formation through the injection borehole at an ambient temperature preferably 25-30° C ±15°C, preferably ±10°C, more preferably ±5°C. As recognized by one of skill in the art, cooler temperatures are capable of dissolving greater amounts of CO2. This aspect of the invention is particularly well-suited for evaporative cooling of the return fluid obtained from the recovery, observation or monitoring well.|[0052] Fixation of the CO2 in the CO2 rich fluid-mixture injected into the geologic formation is, in a preferred embodiment, essentially complete. For example, a CO2 rich fluid-mixture injected into the injection borehole forms a return fluid collected at the return well (observation or monitoring borehole) having an amount of dissolved CO2 that is less than 0.1 wt-%, preferably less than 0.05 wt-%, more preferably less than 0.01% by weight based on the total weight of the return fluid and the CO2. The return fluid may be completely free of CO2.|[0053] In a still further embodiment of the invention the geologic formation is first subject to pretreatment with water or an aqueous solution before the CO2 rich fluid-mixture is injected therein. Pretreatment with water or aqueous solution can enhance initial absorption and fixation of CO2. Treatment with an aqueous solution such as an aqueous acidic solution may enhance CO2 absorption of fixation by forming voids and crevices within the geologic formation thereby providing enhanced fluid flow through the formation and/or otherwise activating the peridotite formation for reaction with CO2.|[0054] Prior mechanical fracturing of the geologic formation is not required. Preferably the CO2 rich fluid-mixture is injected into the geologic formation at pressures substantially less than those necessary in order to mechanically fracture the formation.|[0055] CO2 is dissolved in fluid on surface through a gas dissolution module into the pressurized water stream between the booster pumps and the injection well head. Artificial conservative tracer(s) are used to trace the injected CO2-saturate fluid within the storage reservoir utilizing the monitoring / observation boreholes. Molar ratio of tracers to CO2 are kept constant at the injection well, whereas changes of this ratio in the observation borehole indicates CO2 abatement via reaction with peridotite. The CO2 gas is dissolved once it mixes with the pressurized water stream, where it is carried to the target injection zone. The gas pressure in the pressurized water stream is set to be below or close to the hydrostatic pressure at the target injection depth. The CO2 rich fluid-mixture is then injected through the injection borehole well head. The injection well head is connected through a non-corrosive pipe to a packer system (312) that is installed just above the target injection zone. The packer system (312) hydraulically isolates the column for injection of CO2 rich fluid-mixture into the peridotite rock formation. The injected CO2 rich fluid-mixture is dispersed through the annulus within the peridotite formation where the dissolved CO2 reacts in-situ with the peridotite rocks. The dispersion of the CO2-rich fluid mixture happens via perforated well casing which targets a specific pre-determined permeable layer of the peridotite. Monitoring of both the injected CO2 rich fluid-mixture on surface and the hydraulic pressures at the injection interval is continuously logged for analysis using sensors and a data acquisition system. Samples from the injection borehole below the packed off interval are collected through a membrane system to the surface for continuous dissolved CO2 analysis. The injection well head is fitted with CO2 gas detection devices to monitor any potential leakages of the gas on the surface. This whole process is advantageously powered by a hybrid-renewable system to keep a carbon footprint low and maximize the net amount of CO2 eliminated (see section 2 below).|[0056] The CO2 rich fluid-mixture is preferably injected into the borehole within the target zone by delivery through a steel or polymer tubing string. In this embodiment contact between the borehole wall and/or casing with the CO2 rich fluid-mixture is minimized except for at a location where the borehole is perforated within the target zone of peridotite. The point at which the CO2 rich fluid-mixture is released from the tubing string into the borehole can be determined by using packers at different depths or different positions within the borehole. Preferably packers are set both upstream and downstream of the injection point(s) within the injection borehole at which the CO2 rich fluid-mixture is released from the tubing string into the borehole and through perforations in the borehole casing into the rock formation. Preferably a packer is set above the maximum depth of the target formation and below the minimum depth of the target formation to limit the release of the CO2 rich fluid-mixture into the portion of the borehole which directly corresponds with and is encompassed by a peridotite rock formation.|[0057] In a preferred embodiment of the invention the return fluid formed when the CO2 rich fluid-mixture (e.g., CO2 saturated water) passes through the geologic formation (e.g., peridotite reservoir) is subject to cooling after return to the surface. In order to make good use of renewable resources a portion of the return water is used in an evaporative cooling process. For example, when returning to the surface the return fluid may flow through a manifold system in which the return fluid is divided into at least two portions. A main portion is piped to another location, for example, to a storage tank or directly to the well injection point for further mixing with CO2 and later injection into the injection borehole. The second, typically smaller, portion is transferred to an evaporative cooling apparatus and evaporated. A return fluid pipe used for transferring the main portion of the return fluid may disposed in a second pipe of larger diameter forming an annulus space between the outer surface of the return fluid pipe and the inner surface of the second pipe. The second portion of the return water may then be sprayed or passed into the annulus in the presence of a stream of gas in which the second portion of the return fluid evaporates thereby providing cooling effect to cool the fluid in the return fluid pipe. Preferably, the gas flow used in the evaporative cooling is CO2 which may subsequently be transferred to a CO2 storage facility and/or the well injection point for injection into the geological formation. The gas stream exiting the annulus includes evaporated water and mainly carbon dioxide gas.|[0058] Injection of the CO2 rich fluid-mixture into the injection well may be under conditions permitting effervescence of CO2 from the CO2 rich fluid-mixture. The formation of bubbles in the geologic formation may permit enhanced absorption and/or fixation through effects that include, for example, disruption of water flow as a two-phase mixture and collisions of CO2 bubbles with features of the geologic formation surface.|[0059] The hybrid-renewable system preferably includes a plurality of photovoltaic (PV) cells to generate electricity from sunlight. Electrical storage facilities are typically included. PV panels are preferably mounted over the injection system and over storage tanks. Especially with respect to mounting above the injection system, electrical energy obtained from the PV cells may be used directly thereby avoiding the complexities and expense of long electrical transfer lines.|[0060] Aspects of the invention include portability of injection and renewable energy components. Portability, especially as it relates to the injection system, is especially advantageous for relocation of the injection equipment and energy generating equipment to new locations of geologic material. As a geologic formation of peridotite becomes reacted/saturated with CO2, the efficiency of further CO2 fixation decreases. It is then advantageous to seal the return fluid well (for example by cementing) and relocate injection of the CO2 rich fluid-mixture to an injection point located differently than an initial well.|[0061] Referring to FIGs. 2 and 3, some embodiments of the disclosed subject matter include a continuous injection method and other embodiments show an overview of the CO2 injection system. A submersible pump (SP2) is installed in the observation borehole at depth and is used to pump ground water into an on-surface storage tank (340). SP2 flow rates and pressures preferably match the permeability of the subsurface formation. The on-surface storage tank (340) is equipped with sensors that automate the operation of the SP2 and acts as a buffer between the observation and injection boreholes. In one embodiment, the tank has a volume of at least 5000 L. The on-surface storage tank is also fitted with coupling connections to receive water from different other sources. A set of booster pumps (BP1, BP2) are used in parallel to inject water from the on-surface storage tank (340) at pressure to the injection well (320). The flow rates of the fluid-mixture are adapted to the permeability of the target injection zone at the injection borehole. A permeability test is carried out to determine these rates at the injection borehole prior to injecting CO2 rich fluid-mixture. One or more dosing pumps (DP) is/are used to regulate the flow of a tracer fluid from a tracer tank (360). In one embodiment, said tank has a volume of at least 100 l, and fluorescein is used as the tracer.|[0062] The tracer is injected into the water stream at pressure, in the pipe section between the BPs and the injection well head, using a set of dosing pumps (DPs). The dosing rate is regulated throughout the injection process. The tracer fluid is used to trace the injected CO2 rich fluid-mixture in the subsurface using observation boreholes (333). A gas dissolution module (310) is installed on a flanged pipe section, before the injection well head. CO2 gas is injected at pressure into the water stream. CO2 gas injection pressure is regulated by a mass flow controller device that is connected to a gas manifold. The gas manifold controls the supply of CO2 gas from the CO2 storage tanks at a regulated pressure level. The gas dissolution module is designed to maximize gas transfer efficiencies as well as buffer capacities within the injection pipe column and to release CO2 gas bubbles at <50 µm to maximize bubbles surface area for solubility and to reduce the buoyancy effect. The CO2 rich fluid-mixture is injected into the subsurface through an injection well head on the injection borehole. The injection well head holds the string assembly that is suspended on a supported mechanical system on the surface. The string assembly is composed of (1) Non-corrosive fluid pipes that connect the injection well head on surface to the packer system (312) and acts as the injection column for the CO2 rich fluid-mixture; (2) Submersible pump (SP1) placed on the injection borehole and connected on the string assembly used to pump back the injected CO2 rich fluid-mixture any at given point during the injection process; (3) Shut-In-Tool (SIT, 311) that is used to isolate the injection interval once the CO2 rich fluid-mixture is injected into peridotite formation which acts as a safety measure to prevent any undissolved CO2 gas bubbles from rising back to the surface during any maintenance operations; and (4) packer system or packer module (PS) consists of a water or gas inflation packer that is used to pack off the interval at the target injection zones. The packer is equipped with various sensors to monitor hydraulic pressures of the column above and below the packed off interval as well as the packer pressure. The PS is also set-up with other sensors for live monitoring of the injection zone interval. The interval is packed off at a differential to the column hydrostatic pressure ensuring a proper seal is maintained once hydraulic pressure below the packed off interval begins to increase.|[0063] In addition to conventional tracers, confirmation that CO2 injected into the geological formation is absorbed and fixed can be determining by measuring the CO2/fluid ratio at the well injection point in comparison to the CO2/fluid ratio in the return fluid at a surface return site. The CO2 injected into the geologic formation can be modified to include an amount of nucleotide-labeled material (for example CO2 labeled with 17O or CO2 labeled with 14C) and compared with a corresponding amount (concentration) in the return fluid.|[0064] A fluid recovery well (330) for the return fluid can be located at a distance from the CO2 injection well (320) such that the distance the CO2 rich fluid mixture traverses through the geologic formation is sufficient to absorb and/or fixate substantially all of CO2 in the CO2 rich fluid-mixture. This distance may vary depending on the location of the injection well, the structure of the geologic formation and the availability of water for injecting the CO2 rich fluid-mixture into the geologic formation. A distance of 0.1-10 km, preferably 0.2-5 km, 0.5-1 km or 0.7-0.9 km can be used.|[0065] Referring to FIG. 4, some embodiments of the disclosed subject matter include a renewable energy system that consists of for example, a solar cell module (410), solar inverters (420), an energy storage module comprising a battery system (460), an energy management system, EMS (470), wind turbines (not shown), and a biofuel module, comprising for example synchronized generators (440), a fuel tank (450) for holding biofuel. Further, switchgear (430) and an energy meter (480) is preferably included. The renewable energy system works in such a way that during daytime, solar energy is used to supply the loads to all injection systems on the ground. Excess renewable energy is stored to be used for improved system performance and for operation during night-time. During night-time operation, energy stored is used for supplying the required loads. Based on site consumption, the energy stored would be utilized to supply the night loads throughout the entire night period along with renewable energy sources that can operate at night (Eg; wind turbines and biofuel generators). There is no loss in power while transitioning from solar/off-grid operation to energy storage, the stored energy will instantly take over supply and smoothly transition to energy storage operation only. The hybrid controller will be responsible for communication among the inverters, storage, biofuel generators and the overall transfer of power within the system|[0066] Another preferred embodiment of the present invention is the injection borehole (310, 320) development. This involves increasing wellbore diameter from 16.5 cm to 25 cm for the full depth of the borehole and permanent installation of non-corrosive casing, ideally 7-inch (17.78 cm) in diameter, with slotted sections or screen in the injection zone. Drilling Rate of Penetration (ROP) can be used to interpret rock properties. A slower rate of penetration indicates a requirement for higher fracture stress by the drill bit to break the rock. For rock types that are known to be homogenous this information will serve as an indication for the level of porosity at different depths. Porosity reduces the fracture stress of bulk rock type and therefore increased ROP is indicative to higher porosity.|[0067] Referring to FIG. 5, this confirms that faster ROP above 100 meters below ground level (mbgl) is indicative of a higher level of porosity and therefore a higher water to rock ratio. Below 100 mbgl the porosity is lower and therefore the water to rock ratio is expected to be lower. However, the plot shows distinct regions below 100 mbgl where the ROP increases which indicate the presence of intervals with higher porosity.|[0068] In another preferred embodiment of the present invention, downhole injection assembly system is described. A packer tool (312) is installed to isolate the injection interval from the remaining part of the borehole. This allows for installation of pressure monitoring devices above and below the packer tool (312). A shut-in tool (311) is installed to isolate the injection interval after injection to ensure no upward drift of injected fluid to the top intervals. The submersible pump (SP-1) is used to draw water from the isolated injection interval and for sampling purposes. Downhole injection piping and equipment are pressure rated to withstand injection pressures required. Well head installed constitutes of two ports: 1) Incoming injection fluid and 2) outgoing sampling port. It is noteworthy to mention that a check should carried out for any blockages and remove any existing blockages for the complete depth of the open borehole. A submersible intake pump (SP2) is used in the observation well (333). A submersible pump is used to draw water from the observation well to be used for injection purposes in the injection borehole. The submersible pump is placed at least 60 mbgl to draw water from above the injection interval in injection borehole. This is done to minimize interference in the event of existing subsurface connectivity between the two wellbores. The submersible pump is sized on the following flow basis: provide a flow rate of a minimum of 0.1 L/s and a minimum of 8640 L/day under the recommended operating schedule. The submersible pump is sized on the following pressure basis: placement depth is a minimum of 60 mbgl (meters below ground level); pumping head must be sufficient to deliver water to surface at ease. Submersible pumps cannot operate continuously for extended period. Therefore, the observation well water will be supplied with temporarily stored water in a buffer tank to counteract the intermittent nature of submersible pumps.|[0069] In another preferred embodiment of the present invention a water buffer tank is described. The water buffer tank or tanks will hold water from observation wells or from another source to counteract pumping intermittency, flow intermittency, stabilize pressure and for additional process control and operational reasons. Sizing of the buffer tank is dependent on the selection of the submersible pump and is made on the following basis: 1) the tank holds sufficient capacity to allow the submersible pump to deliver the daily required volumes following the recommended hours of operation schedule; and 2) the tank should hold sufficient capacity to allow for continuous and uninterrupted draw of at least 0.1 L/s for injection. In a test run performed by the present inventors, a buffer tank capacity of 5500 L was chosen.|[0070] The buffer tank also plays a critical role of dampening pressure fluctuation caused by natural changes in water levels in the observation borehole and will therefore allow for a stable pressure supply by the injection pumps. The injection pump/s are selected for continuous and uninterrupted operation. The sizing of the pumps are made on the following basis: 1) flow rate set at a minimum of 0.1 L/s; 2) sufficient overpressure to cover hydrostatic head at the injection interval, major and minor head losses due to the system assembly, and account for pressure build up to allow flow through the injection zone is done through energy balance equation used to calculate head loss in system and Darcy's law used to determine flow into the injection zone by assuming linear cylindrical outward flow; and 3) provide a pressure high enough to ensure solubility of dissolved CO2 on surface at steady state flow conditions. A dosing pump (DP1) is used to inject set volume (at least 5 mL/min) of liquid conservative tracers, e.g. fluorescein, into along with the injection fluid. Dosing is done inline after the injection pumps / booster pumps. Due to the dynamic changes in the subsurface pressure conditions after the start of injection flow rate is expected to change over time to reflect the change in conditions. The water flowmeter will record changes in the injected fluid flow rate over injection time to monitor the system behavior with respect to subsurface pressure and to allow for accurate accounting of total injected volumes and to assist with dynamic data interpretation. Preferably, an electromagnetic flow meter is selected for its uniform behavior, responsive reading time, un-interruption to flow and due to the homogenous nature of the injected fluid that allows for consistent magnetic behavior and therefore consistent flow reading accuracy. The flow meter is calibrated specifically for the project application to ensure the accuracy of the meter for the expected flow conditions.|[0071] Another preferred embodiment of the present invention is a CO2 injection system development. The Automatic CO2 gas switchover manifold is used to stabilize and regulate the pressure from CO2 tanks. CO2 tank pressure gradually decreases as the contained gas is depleted and due to the sensitive thermodynamic behavior of gas temperature swings between day and night has a significant impact on tank supply pressure. Further the expansion of the gas through various valves and through the pipes also associate with temperature changes and consequently pressure changes. To allow for accurate and controlled pressure delivery the manifold regulates the delivery pressure from tanks to a selected setpoint. The manifold also ensures uninterrupted CO2 supply by operating one wing (301) and keeping the second wing (302) on standby. Once the delivery pressure from the primary wing is not capable of meeting the target setpoint the manifold automatically switches to the secondary standby wing. Gas flow is difficult to regulate due to the impact of temperature upstream and downstream pressure on the flow rate. The gas flow controller will adjust the flow to account for all gas flow fluctuation to maintain a stable flow rate of a minimum of 1.3 g/s. A gas dissolution module is used to mix CO2 into the water.|[0072] A gas dissolution system (310) can be used to maximize the gas liquid contact surface area to minimize gas dissolution time and to ensure complete dissolution of CO2 in the injected water. This system is placed after the injection pump as higher pressures promote higher gas solubility. The system is designed to dissolve gas with a bubble diameter less than 100 µm and is specifically designed and tuned for the project application accounting for both water and gas flow rates and pressures. The design of the system also accounts for the gas pressure drop across the system to balance with the maximum delivery pressure available from the manifold and additional pressure drops in the gas delivery system, to ensure flow into the high-pressure water line. The housing of the system is designed to accommodate all components with minimal interruption to water flow, provides easy internal access for servicing purposes and allows for slower flow velocity so that the dissolution residence time matches the fluid residence time in the unit.|[0073] In another preferred embodiment include a monitoring system. Monitoring includes a complete water quality testing, pH, total dissolved solids (TDS), electrical conductivity (EC), temperature, Oxidation Reduction Potential (ORP) and other physical properties. A sample from borehole water has been collected after drilling activity for complete water quality testing by an independent laboratory. A submersible pump placed at a minimum of 60 mbgl was used to collect water for pH, EC, TDS, Temperature and ORP on site. An additional submersible pump was placed at a minimum of 60 mbgl used to collect samples to test for cations, anions, alkalinity, and dissolved CO2. In addition, monitoring system also included the injected conservative tracers to monitor the change of the molar ratio of CO2 to tracers, which was kept constant in the injection well. Changes in this ratio will indicate CO2-water-rock reactions and thus CO2 abatement. In addition, utilizing natural tracers such as stable carbon, strontium, magnesium and calcium isotopes, it is possible to determine the reactivity of the peridotite system to mineralize the injected CO2.|[0074] In another preferred embodiment of the present invention, the fluid flow path between the injected borehole and the observation borehole are natural fractures that extend in other directions than upward or downward or in case of limiting natural fractures, a fracture network that has been induced through permeability enhancement.|EXAMPLE|[0075] In a pilot scale experiment carried out in the Samail Ophiolites in the Sultanate of Oman and supervised by the inventors, a system was constructed as schematically shown in FIGs 3 and 10. Two boreholes (1020, and 1030) were drilled into the rock until a peridotite layer (P) was reached. The first borehole (1020) was fitted with well casing which was perforated (See FIG 11) at the targeted areas for peridotite mineralization. A packer (1012) was used to isolate the peridotite layer (P) for targeted injection of the CO2 - water mixture. A submersible pump (SP1) located in the borehole (1020) above the packer was used to recoup the injected fluid mixture after an incubation period for sampling and analysis, to prove occurrence of mineralization (M). A submersible pump (SP2), in the opposite borehole (1030), was used to pump groundwater for injection into the injection borehole.|[0076] CO2 was fully dissolved in the groundwater on the surface using a gas dissolution module (310) at a pre-defined CO2 to water ratio. A conservative tracer (here sodium fluorescein) was metered into the water injection stream using a dosing pump, operated at a specific rate that accounted for dilution in the subsurface. The CO2 saturated fluid was injected via a non-corrosive pipe to the hydraulically isolated target injection interval in the first borehole (1020). A monitoring borehole (not shown) that was hydraulically connected to the injection borehole via a natural fracture network in the peridotite reservoir, was utilized for estimating the CO2 mineralization capacity of said reservoir rock. Samples were also taken in the first borehole (1020) in an upper section above the packer (1012) peridotite layer (P).|[0077] A monitoring equipment was used to monitor the degree of CO2 abatement via peridotite-water reactions, utilizing the molar ratio of CO2 to said conservative tracer. Using the measured concentration of said conservative tracer in the injected fluid and the fluid retrieved in the monitoring borehole allowed calculating the dilution of the injected fluid with ambient reservoir groundwater via dispersion. Changes in the conservative tracer to CO2 molar ratio from the injection borehole (which is fixed for said injection) to the observation borehole indicated CO2-peridotite reactions and thus a loss of CO2 along the said flow path. CO2 mineralization could be quantified by monitoring the dissolved CO2 content in the injected fluid and in the observation borehole via said membrane system. Decreased dissolved CO2 concentration in the observation borehole fluids compared to the initial concentration in the injection borehole clearly indicated that an amount of CO2 was sequestered.|[0078] The experiment was performed during a period of six days, and the measured results are shown in FIGs 5 - 9. The results indicated that the system remained stable and operational during the test period. Family Number|(103686458)|103686458|Abstract|(US12168610 B2)|The present invention provides a system and method to mineralize CO2 into peridotite rocks in a controlled and efficient manner removing carbon permanently from the atmosphere. Carbon dioxide sequestration into peridotite rocks happens naturally by means of natural weathering. However, this process is so slow and might take thousands of years to transform considerable amount of CO2 into carbonate rocks. The present invention, however, shortens the time of mineralization considerably in a controlled and quantifiable manner. This is typically done by injecting CO2 into peridotite rock formation and creating an efficient reaction pathways and conditions for the mineralization reaction to happen and therefore store CO2 by conversion into magnesite (MgCO3) and calcite (CaCO3).|(EP4134513 C0)|Here is provided a system and method to mineralize CO2 into peridotite rock formations in situ in a controlled and efficient manner removing carbon permanently from the atmosphere. Carbon dioxide sequestration into peridotite rocks happens naturally by means of natural weathering. This process is slow and might take thousands of years to transform considerable amount of CO2 into carbonate rocks. The present method disclosed herein shortens the time of mineralization considerably in a controlled and quantifiable manner. This is typically done by injecting CO2 into peridotite rock formation and creating efficient reaction pathways and conditions for the mineralization reaction to happen and therefore store CO2 by conversion into magnesite (MgCO3) and calcite (CaCO3).|(JP7384477 B2)|PROBLEM TO BE SOLVED: To provide systems and methods for the insitu mineralization of CO2 into peridotite formations in a controlled and efficient manner that permanently removes carbon from the atmosphere.SOLUTION: Carbon dioxide isolation within peridotite occurs naturally through natural weathering. This process is slow and can take thousands of years to convert significant amounts of CO2 into carbonate rocks. The method disclosed herein significantly reduces the time of mineralization M in a controlled and quantifiable manner. This is generally done by injecting CO2 into peridotite formation P to create efficient reaction pathways and conditions for the mineralization reactions to occur, and thereby is carried out by storing CO2 by conversion to magnolite (MgCO3) and calcite (CaCO3).SELECTED DRAWING: Figure 1COPYRIGHT: (C)2023,JPO&INPIT|(AU2022209209 A1)|Here is provided a system and method to mineralize C02 into peridotite rock formations in situ in a controlled and efficient manner removing carbon permanently from the atmosphere. Carbon dioxide sequestration into peridotite rocks happens naturally by means of natural weathering. This process is slow and might take thousands of years to transform considerable amount of C02 into carbonate rocks. The present method disclosed herein shortens the time of mineralization considerably in a controlled and quantifiable manner. This is typically done by injecting C02 into peridotite rock formation and creating efficient reaction pathways and conditions for the mineralization reaction to happen and therefore store C02 by conversion into magnesite (MgCO3) and calcite (CaCO3). (Fig. 1) Ii' iiii~II _ _ _ _ _ _ ~ .4' -|(CA3191648 A1)|The present invention provides a system and method to mineralize CO2 into peridotite rocks in a controlled and efficient manner removing carbon permanently from the atmosphere. Carbon dioxide sequestration into peridotite rocks happens naturally by means of natural weathering. However, this process is so slow and might take thousands of years to transform considerable amount of CO2 into carbonate rocks. The present invention, however, shortens the time of mineralization considerably in a controlled and quantifiable manner. This is typically done by injecting CO2 into peridotite rock formation and creating an efficient reaction pathways and conditions for the mineralization reaction to happen and therefore store CO2 by conversion into magnesite (MgCO3) and calcite (CaCO3).|(ES2997244 T3)|Here is provided a system and method to mineralize CO2 into peridotite rock formations in situ in a controlled and efficient manner removing carbon permanently from the atmosphere. Carbon dioxide sequestration into peridotite rocks happens naturally by means of natural weathering. This process is slow and might take thousands of years to transform considerable amount of CO2 into carbonate rocks. The present method disclosed herein shortens the time of mineralization considerably in a controlled and quantifiable manner. This is typically done by injecting CO2 into peridotite rock formation and creating efficient reaction pathways and conditions for the mineralization reaction to happen and therefore store CO2 by conversion into magnesite (MgCO3) and calcite (CaCO3).(From EP4134513 A1)|(AE20226000645 A1)|The present invention provides a system and method to mineralize CO2 into peridotite rocks in a controlled and efficient manner removing carbon permanently from the atmosphere. Carbon dioxide sequestration into peridotite rocks happens naturally by means of natural weathering. However, this process is so slow and might take thousands of years to transform considerable amount of CO2 into carbonate rocks. The present invention, however, shortens the time of mineralization considerably in a controlled and quantifiable manner. This is typically done by injecting CO2 into peridotite rock formation and creating an efficient reaction pathways and conditions for the mineralization reaction to happen and therefore store CO2 by conversion into magnesite (MgCO3) and calcite (CaCO3).|CPC codes|(US12168610 B2)|C01F-005/24|C01F-011/18/1|(EP4134513 C0)|C01F-005/24|C01F-011/18/1|(JP7384477 B2)|C01F-005/24|C01F-011/18/1|(AU2022209209 A1)|C01F-005/24|C01F-011/18/1|(ES2997244 T3)|C01F-005/24|C01F-011/18/1|IPC codes|(US12168610 B2)|C01F-005/24|C01F-011/18|(CA3191648 A1)|B01D-053/14|B01D-053/62|Title|(US20230038447 A1)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(US12168610 B2)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(EP4134513 A1)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(EP4134513 B1)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(EP4134513 C0)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(JP7384477 B2)|System and method for constant carbon dioxide sequestration using renewable energy sources|(AU2022209209 A1)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(CA3191648 A1)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(ZA202208785 B)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(ES2997244 T3)|System and method for permanent carbon dioxide sequestration using a renewable energy source|(AE20226000645 A1)|System and method for permanent carbon dioxide sequestration using a renewable energy source| Civil engineering|Environmental technology|Handling|Materials, metallurgy C01F-005/24|C01F-011/18/1|E21B-041/00/64|E21B-043/16/4|Y02C-020/40 C01F-005/24|C01F-011/18/1|E21B-041/00/64|E21B-043/16/4|Y02C-020/40 B01D-053/14|B01D-053/62|B65G-005/00|C01F-005/24|C01F-011/18|E21B-041/00|E21B-043/16|E21B-043/40 B01D-053/14|B01D-053/62|B65G-005/00|C01F-005/24|C01F-011/18|E21B-041/00|E21B-043/16|E21B-043/40 WO202576520|WO202536939|WO202540953;WO202540953|CN120087975|WO2024220438;WO2024220438|CN117231169|CN116359471|US20250305392|US20250283391|US20240110464|US20230323755|US12297730|US12480383|WO202540953;WO202540953|US12551845|US12534979|US12467339|CN117108273B|GB2632672|US20250052151|US12116868 WO202576520 114137073 WHO=Examiner SELF=N CAT=Y|WO202536939 106750860 WHO=Examiner SELF=N CAT=X|WO202540953 113546807 WHO=Examiner SELF=Y CAT=I CAT=A CAT=Y|CN120087975 114760660 WHO=Examiner SELF=N CAT=A|WO2024220438 111908472 WHO=Examiner SELF=N CAT=A|CN117231169 107765318 WHO=Examiner SELF=N CAT=A|CN116359471 105563865 WHO=Examiner SELF=N CAT=A|US20250305392 116115464 WHO=Examiner SELF=N CAT=103|US20250283391 115879307 WHO=Examiner SELF=N CAT=103|US20240110464 109083548 WHO=Examiner SELF=N CAT=103|US20230323755 106773894 WHO=Examiner SELF=N CAT=103|US12297730 114471733 WHO=Examiner SELF=N CAT=102|US12480383 110558061 WHO=Examiner SELF=N|WO202540953 113546807 WHO=Applicant SELF=Y|US12551845 112020354 WHO=Examiner SELF=N|US12534979 116115464 WHO=Examiner SELF=N|US12467339 115879307 WHO=Applicant SELF=N|CN117108273B 107449904 WHO=Examiner SELF=N|GB2632672 106750860 WHO=Examiner SELF=N|US20250052151 113257602 WHO=Examiner SELF=N|US12116868 109083548 WHO=Examiner SELF=N US20210261451|US20170009561|JP2015078677|JP2009011964|WO2020234464|US20140186119|US20120164042|US20090202304|US20040200618|WO2020234464|WO2020234464|CN108658104|CN108658104|US9266061|US9266061|US9193594|US9193594|US20110162842|US8524152|US8524152|JP2007283279|JP2007283279|US6325147|US4632601|US4441555 US20210261451 95805831 WHO=Examiner SELF=N CAT=DBL|US20170009561 75117838 WHO=Examiner SELF=N CAT=A|JP2015078677 69267270 WHO=Examiner SELF=N CAT=A|JP2009011964 32866306 WHO=Examiner SELF=N CAT=A|WO2020234464 91642681 WHO=Examiner SELF=N CAT=103|US20140186119 72113167 WHO=Examiner SELF=N CAT=103|US20120164042 1874736 WHO=Examiner SELF=N CAT=103|US20090202304 32694401 WHO=Examiner SELF=N CAT=103|US20040200618 43999183 WHO=Examiner SELF=N CAT=103|WO2020234464 91642681 WHO=Applicant SELF=N|WO2020234464 91642681 WHO=Applicant SELF=N|CN108658104 81640656 WHO=Applicant SELF=N|CN108658104 81640656 WHO=Applicant SELF=N|US9266061 44416104 WHO=Applicant SELF=N|US9266061 44416104 WHO=Applicant SELF=N|US9193594 1874736 WHO=Applicant SELF=N|US9193594 1874736 WHO=Applicant SELF=N|US20110162842 1848531 WHO=Examiner SELF=N|US8524152 4164374 WHO=Applicant SELF=N|US8524152 4164374 WHO=Applicant SELF=N|JP2007283279 32663261 WHO=Applicant SELF=N|JP2007283279 32663261 WHO=Applicant SELF=N|US6325147 4036279 WHO=Examiner SELF=N|US4632601 19119825 WHO=Examiner SELF=N|US4441555 42502854 WHO=Examiner SELF=N ||JP2009011964; JP2015078677; US20170009561||XP055970830; XP055970876; XP037108639; XP055970885; XP008150329; US9193594; US8524152; US9266061; JP2007283279; CN108658104; WO2020234464|||US20120164042; US20140186119; US20040200618; WO2020234464; US20090202304; US20210261451; US4441555; US4632601; US6325147; US20110162842; US8524152; US9193594; US9266061; CN108658104; JP2007283279; WO2020234464 (EP4134513)|Applicant references|-CLARK DEIRDRE E. ET AL: "CarbFix2: CO2 and H2S mineralization during 3.5?years of continuous injection into basaltic rocks at more than 250?°C", GEOCHIMICA ET COSMOCHIMICA ACTA., vol. 279, 1 June 2020 (2020-06-01), US, pages 45 - 66, XP055970830, ISSN: 0016-7037, DOI: 10.1016/j.gca.2020.03.039|-RAGUL HARI S ET AL: "Carbon Capture and Storage Using Renewable Energy Sources: A Review", IOP CONFERENCE SERIES: EARTH AND ENVIRONMENTAL SCIENCE, vol. 573, no. 1, 1 October 2020 (2020-10-01), pages 012004, XP055970876, ISSN: 1755-1307, Retrieved from the Internet &lt;URL:https://iopscience.iop.org/article/10.1088/1755-1315/573/1/012004/pdf&gt; [retrieved on 20221013], DOI: 10.1088/1755-1315/573/1/012004|-HANAK DAWID P ET AL: "Linking renewables and fossil fuels with carbon capture via energy storage for a sustainable energy future", FRONTIERS OF CHEMICAL SCIENCE AND ENGINEERING, HIGHER EDUCATION PRESS, HEIDELBERG, vol. 14, no. 3, 19 December 2019 (2019-12-19), pages 453 - 459, XP037108639, ISSN: 2095-0179, [retrieved on 20191219], DOI: 10.1007/S11705-019-1892-2|-SN BJÖRNSDÓTTIR SANDRA O. ET AL: "Carbon dioxide storage through mineral carbonation", NATURE REVIEWS, 20 January 2020 (2020-01-20), XP055970885, DOI: doi.org/10.1038/ s43017-019-0011-8|-PETER B. KELEMENJIIRG MATTER: "In situ carbonation of peridotite for C0 storage", PNAS, vol. 105, no. 45, 11 November 2008 (2008-11-11), pages 17295 - 17300, XP008150329, DOI: 10.1073/pnas.0805794105|-Peter B. Kelemen and Jürg Matter, In situ carbonation of peridotite for CO2 storage, PNAS November 11, 2008 105 (45) 17295-17300|-D.E.Clark et al. ("CarbFix2: CO2 and H2S mineralization during 3.5 years of continuous injection into basaltic rocks at more than 250°C" by Deidre E. Clark et al., published in Geochimica et Cosmochimica Acta, volume 279, 1 June 2020, pages 45-66||(US12168610)|Examiner references|-Japanese Office Action issued Jun. 27, 2023 in Japanese Patent Application No. 2022-121235 (with English language translation), 4 pages.||||||| GRANTED (EP4134513)|GRANTED|(US12168610)|GRANTED|(JP7384477)|GRANTED|(ES2997244)|GRANTED|(ZA202208785)|GRANTED|(AEP6000645/2022)|PENDING|(CA3191648)|PENDING|(AU2022209209)|PENDING ALIVE (EP4134513)|ALIVE|(US12168610)|ALIVE|(JP7384477)|ALIVE|(ES2997244)|ALIVE|(ZA202208785)|ALIVE|(AEP6000645/2022)|ALIVE|(CA3191648)|ALIVE|(AU2022209209)|ALIVE (EP4134513)|LEGAL DETAILS FOR EP4134513|Actual or expected expiration date=2042-05-24|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-05-24|Event code=EP/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=EP EP22175231|Application date=2022-05-24|Standardized application number=2022EP-0175231|Event publication 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Box 27834 , CITY=115 93 Stockholm , COUNTRY=SE , REG=101410948|(EP4134513)|NAME=Kransell & Wennborg KB P.O. Box 27834 , CITY=115 93 Stockholm , COUNTRY=SE , REG=101410948|(US12168610)|NAME=Oblon, McClelland, Maier & Neustadt, L.L.P.|(JP7384477)|NAME=SUZUYE & SUZUYE , REG=110003708NAME=KURATA, Masatoshi et al. , REG=100108855NAME=INOUE, Tadashi , REG=100179062NAME=KYOKUTO RESIN:KK , REG=100199565NAME=Naoyuki Yato , REG=100212705NAME=Ikuharu Ohya , REG=100219542NAME=KONO NAOKI , REG=100153051NAME=KANEKO SANAE , REG=100162570|(JP2023024948)|NAME=SUZUYE & SUZUYE , REG=110003708NAME=KURATA, Masatoshi et al. , REG=100108855NAME=INOUE, Tadashi , REG=100179062NAME=KYOKUTO RESIN:KK , REG=100199565NAME=Naoyuki Yato , REG=100212705NAME=Ikuharu Ohya , REG=100219542NAME=KONO NAOKI , REG=100153051NAME=KANEKO SANAE , REG=100162570|(AEP6000645/2022)|NAME=Dennemeyer and Associates S A Regal Tower office 608, Al saada street, business bay, Dubai , COUNTRY=AE , REG=704210|(CA3191648)|NAME=GOWLING WLG (CANADA) LLP , COUNTRY=CA|(AU2022209209)|NAME=Pizzeys Patent and Trade Mark Attorneys Pty Ltd GPO Box 1374 , CITY=Brisbane , STATE=QLD , POSTCODE=4001 , COUNTRY=AU |(EP4134513)|OM; OM; OM|(EP4134513)|GB|(US12168610)|OM; OM; OM|(US20230038447)|OM; OM; OM|||||(AEP6000645/2022)|OM; OM; OM|(CA3191648)|OM; OM; OM| (EP4134513)|NAME=HASAN, Talal|NAME=KHIMJI, Karan|NAME=TASFAI, Ehab|(EP4134513)|NAME=HASAN, Talal, CITY=PC 116 Muscat, COUNTRY=OM |NAME=KHIMJI, Karan, CITY=PC116 Muscat, COUNTRY=OM |NAME=TASFAI, Ehab, CITY=PC 116 Muscat, COUNTRY=OM|(EP4134513)|NAME=PROTOSTAR GROUP LIMITED 100 Cannon Street, CITY=London EC4N 6EU, COUNTRY=GB|(US12168610)|NAME=Hasan Talal, CITY=Muscat, COUNTRY=OM |NAME=Khimji Karan, CITY=Muscat, COUNTRY=OM |NAME=Tasfai Ehab, CITY=Muscat, COUNTRY=OM|(US20230038447)|NAME=Hasan Talal, CITY=Muscat, COUNTRY=OM |NAME=Khimji Karan, CITY=Muscat, COUNTRY=OM |NAME=Tasfai Ehab, CITY=Muscat, COUNTRY=OM|(JP7384477)|NAME=TALAL HASAN|NAME=KARAN KHIMJI|NAME=EHAB TASFAI|(JP2023024948)|NAME=TALAL HASAN|NAME=KARAN KHIMJI|NAME=EHAB TASFAI|(ES2997244)|NAME=HASAN, Talal|NAME=KHIMJI, Karan|NAME=TASFAI, Ehab|(ZA202208785)|NAME=TALAL HASAN|NAME=KARAN KHIMJI|NAME=EHAB TASFAI|(AEP6000645/2022)|NAME=Talal Hasan PO Box 117, PC 116, Muscat, COUNTRY=OM |NAME=Karan Khimji PO Box 117, PC 116, Muscat, COUNTRY=OM |NAME=Ehab Tasfai PO Box 117, PC 116, Muscat, COUNTRY=OM|(CA3191648)|NAME=HASAN, TALAL, COUNTRY=OM |NAME=KHIMJI, KARAN, COUNTRY=OM |NAME=TASFAI, EHAB, COUNTRY=OM|(AU2022209209)|NAME=HASAN, Talal|NAME=KHIMJI, Karan|NAME=TASFAI, Ehab 12 8 Titre: (EP4134513)|System and method for permanent carbon dioxide sequestration using a renewable energy source Résumé: (EP4134513)|Here is provided a system and method to mineralize CO2 into peridotite rock formations in situ in a controlled and efficient manner removing carbon permanently from the atmosphere. Carbon dioxide sequestration into peridotite rocks happens naturally by means of natural weathering. This process is slow and might take thousands of years to transform considerable amount of CO2 into carbonate rocks. The present method disclosed herein shortens the time of mineralization considerably in a controlled and quantifiable manner. This is typically done by injecting CO2 into peridotite rock formation and creating efficient reaction pathways and conditions for the mineralization reaction to happen and therefore store CO2 by conversion into magnesite (MgCO3) and calcite (CaCO3). 69 Abstract gpt-4o-mini yes The article describes a method for accelerating the mineralization of CO2 into carbonates using peridotite, which aligns with the topic of enhanced weathering and carbon sequestration.
73 CN202011213586 CN202011213586 CN112246215 92402840 CN112246215 A 2021-01-22 [CN112246215] 2020-11-04 2020-11-04 2021-01-22 (CN112246215)|2023-03-10 (CN112246215)|Method for preparing adsorbing material for water treatment by taking coal gangue as raw material (CN112246215)|A method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material is characterized by comprising the following steps: A1, coal gangue micronization treatment: crushing blocky coal gangue into coal gangue powder with the particle size of less than 45 microns by adopting mechanical crushing; A2, calcining carbon removal and activation treatment: calcining the coal gangue powder obtained in the step A1 at a high temperature of 500800 DEG C, keeping the temperature for 60180 minutes, and naturally cooling to obtain calcined coal gangue powder; A3, mixing thecalcined coal gangue powder obtained in the step A2 with water to prepare slurry, wherein the mass ratio of the calcined coal gangue powder to the water is 1: (3-10); then performing stirring and reacting for 12-48 hours in a pressure reaction kettle at 180-250 DEG C, cooling, then carrying out solid-liquid separation by adopting a centrifugal machine, and then performing drying and grinding to finally obtain the coal gangue adsorbing material for water treatment. HENAN POLYTECHNIC UNIVERSITY (CN112246215)|HENAN POLYTECHNIC UNIVERSITY ([CN]) ZHANG QIAN|ZHANG YUDE|CHEN ZIYI|YIN SHUAIJUN|KANG YAMIN|ZHAO XIAOLEI|FENG ZHAOXIANG (CN112246215)|ZHANG QIAN|ZHANG YUDE|CHEN ZIYI|YIN SHUAIJUN|KANG YAMIN|ZHAO XIAOLEI|FENG ZHAOXIANG (CN112246215)|GUO ZHONGMIN;ZHENGZHOU ZHONGMIN PATENT AGENT CO., LTD|Reg. Nb: 41110 (CN112246215)|Compared with the prior art, the method has the advantages of simple process, realization of full utilization of the coal gangue resource, product macro particle size of 10-20 microns, nano-porous form of the micro secondary structure, pore size of 2-15 nanometers, nano-micron multilevel structure and easy realization of industrial production.| (CN112246215)|1. A method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material is characterized by comprising the following steps: the method comprises the following steps:a1, coal gangue micronization treatment: crushing the massive coal gangue into coal gangue powder with the granularity less than 45 microns by adopting mechanical crushing;a2, calcining to remove carbon, and activating: calcining the coal gangue powder obtained in the step A1 at the high temperature of 500-800 ℃, keeping the temperature for 60-180 minutes, and naturally cooling to obtain calcined coal gangue powder;a3, mixing the calcined coal gangue powder obtained in the step A2 with water to prepare slurry, wherein the mass ratio of the calcined coal gangue powder to the water is 1: 3-10; and then stirring and reacting in a pressure reaction kettle at the temperature of 180-250 ℃ for 12-48 hours, cooling, performing solid-liquid separation by using a centrifugal machine, drying, and grinding to finally prepare the coal gangue adsorbing material for water treatment.| (CN112246215)|The invention aims to provide a method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material aiming at the defects in the prior coal gangue utilization technology.|The invention relates to the technical field of solid waste resource utilization and material preparation, in particular to a method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material.|The object of the invention can be achieved by the following technical measures:| (CN112246215)|COAL GANGUE(100,38)|WATER TREATMENT(100,14)|COAL GANGUE POWDER CALCINATION(100,10)|RAW MATERIAL(100,8)|ADSORBENT MATERIAL(100,6)|COAL GANGUE POWDER(90,18)|MASSIVE COAL GANGUE(82,3)|COAL GANGUE MICRONIZATION TREATMENT(80,3)|CALCINED COAL GANGUE(69,7)|COAL GANGUE RESOURCE(64,1)|COAL GANGUE UTILIZATION(62,1)|CRUSHING(28,3)|GRANULARITY(27,3)|NANOMICRON MULTILEVEL STRUCTURE(26,1)|RESOURCE UTILIZATION(25,3)|SOLID WASTE RESOURCE UTILIZATION(22,1)|PRIOR COAL GANGUE UTILIZATION(21,1)|TECHNICAL MEASURE(21,1)|FULL UTILIZATION(20,1)|PRESSURE REACTION KETTLE(19,5)|SLURRY(18,3)|DEFECT(17,1)|COAL GANGUE ADSORPTION MATERIAL(14,6)|INDUSTRIAL PRODUCTION(14,2)|CENTRIFUGAL MACHINE(13,6)|PORE(13,1)|200 320M2THE PORE VOLUME(11,1)|COAL GANGUE ADSORBENT PORE(11,1)|COAL GANGUE MICRO POWDER(10,4)|PORE DIAMETER(10,3)|COAL GANGUE ADSORPTION PURIFICATION(10,1)|COAL GANGUE MICROPOWDER(10,1)|PRODUCT MACRO PARTICLE SIZE(10,1)|MICRO SECONDARY STRUCTURE(9,1)|SOLID LIQUID SEPARATION(8,6)|CALCINATION DECARBONIZATION ACTIVATION(8,1)|JAW HAMMER CRUSHER(8,1)|MASS RATIO(7,6)|MICRONIZATION COMPREHENSIVE TREATMENT(7,1)|SPHERICAL PARTICLE(6,3)|200 320M2THE COAL GANGUE(6,2)|ORGANIC DYE(6,2)|SOLID WASTE(6,2)|COAL GANGUE PORE VOLUME(6,1)|COAL GANGUE TREATMENT(6,1)|NANOSCALE PARTICLE SPHERICITY(6,1)|MICRO POWDER PARTICLE(5,5)|HEAVY METAL ION(5,2)|ACTIVATION CALCINATION(5,1)|AUXILIARY CALCINATION(5,1)|COAL GANGUE COMPONENT(5,1)|LEACHING RESIDUAL WASTE RESIDUE(5,1)|NANOSCALE STACK(5,1)|POROUS ADSORPTION(5,1)|WASTEWATER POLLUTION(5,1)|RECONSTRUCTION(4,2)|ACTIVATED COAL GANGUE POWDER(4,1)|CEMENT DOPING(4,1)|EXTENSIVE TREATMENT(4,1)|INORGANIC MINERAL(4,1)|AVERAGE GRAIN DIAMETER(3,2)|JAW CRUSHER(3,2)|CARBONIZING COAL(3,1)|COAL GANGUE ADSORBENT MATERIAL(3,1)|GENERATED WASTE RESIDUE(3,1)|LEACHING TREATMENT(3,1)|MINERAL CONTENT(3,1)|REACTION KETTLE(3,1)|TRANSPORTATION COST(3,1)|TRICHLOROALUMANE(3,1)| (CN112246215)|1. A method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material is characterized by comprising the following steps: the method comprises the following steps:|a1, coal gangue micronization treatment: crushing the massive coal gangue into coal gangue powder with the granularity less than 45 microns by adopting mechanical crushing;|a2, calcining to remove carbon, and activating: calcining the coal gangue powder obtained in the step A1 at the high temperature of 500-800 ℃, keeping the temperature for 60-180 minutes, and naturally cooling to obtain calcined coal gangue powder;|a3, mixing the calcined coal gangue powder obtained in the step A2 with water to prepare slurry, wherein the mass ratio of the calcined coal gangue powder to the water is 1: 3-10; and then stirring and reacting in a pressure reaction kettle at the temperature of 180-250 ℃ for 12-48 hours, cooling, performing solid-liquid separation by using a centrifugal machine, drying, and grinding to finally prepare the coal gangue adsorbing material for water treatment.|2. The method for preparing the adsorbing material for water treatment by using the coal gangue as the raw material according to claim 1, wherein the method comprises the following steps: the diameter of the coal gangue adsorption material is 10-20 microns, and the specific surface area is 200-320m2The pore volume reaches 0.4-0.7cm3/g, the pore diameter is 2-15nm, and organic dyes and heavy metal ions in the wastewater can be simultaneously adsorbed and removed. (CN112246215)|TECHNICAL FIELD|[0002] The invention relates to the technical field of solid waste resource utilization and material preparation, in particular to a method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material.|BACKGROUND ART|[0004] The coal gangue is solid waste in the coal washing and selecting process, and the main components of the coal gangue are silicate minerals and a small amount of coal carbon. At present, the resource utilization approach of the coal gangue mainly comprises coal gangue power generation, but only the coal gangue with higher calorific value can be utilized, and a large amount of generated waste residues need to be further treated; the coal gangue is used as a building auxiliary material for paving, cement doping, brick making and the like, but has low additional value and high transportation cost and can only be utilized nearby. Some methods adopt gravity separation and flotation to extract kaolinite, pyrite and the like in the ore with certain mineral content reaching certain grade. In some researches, chemical treatment of coal gangue is adopted, aluminum chloride is prepared to serve as a water treatment agent, strong acid and strong alkali are adopted in the preparation process for leaching treatment, certain environmental hazards are caused, and a large amount of leaching residual waste residues are generated.|[0005] Disclosure of Invention|[0006] The invention aims to provide a method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material aiming at the defects in the prior coal gangue utilization technology. The invention completely does not use chemical agents, and prepares a novel coal gangue adsorption purification material with a nano-level porous structure by taking coal gangue as a raw material. The preparation method is environment-friendly, the coal gangue is completely converted into the adsorption water purification material, and no secondary waste is generated in the preparation process.|[0007] The object of the invention can be achieved by the following technical measures:|[0008] the method for preparing the adsorbing material for water treatment by using the coal gangue as the raw material comprises the following steps:|[0009] a1, coal gangue micronization treatment: crushing the massive coal gangue into coal gangue powder with the granularity less than 45 microns by adopting mechanical crushing;|[0010] a2, calcining to remove carbon, and activating: calcining the coal gangue powder obtained in the step A1 at the high temperature of 500-800 ℃, keeping the temperature for 60-180 minutes, and naturally cooling to obtain calcined coal gangue powder;|[0011] a3, mixing the calcined coal gangue powder obtained in the step A2 with water to prepare slurry, wherein the mass ratio of the calcined coal gangue powder to the water is 1: 3-10; and then stirring and reacting in a pressure reaction kettle at the temperature of 180-250 ℃ for 12-48 hours, cooling, performing solid-liquid separation by using a centrifugal machine, drying, and grinding to finally prepare the coal gangue adsorbing material for water treatment.|[0012] The coal gangue adsorption material for water treatment has the diameter of 10-20 microns and the specific surface area of 200-320m2The coal gangue micro powder particles have rich hierarchical porous structures, the pore volume of the coal gangue micro powder particles reaches 0.4-0.7cm3/g, and the pore diameter is 2-15 nm.|[0013] The invention has the following beneficial effects:|[0014] the invention adopts the calcining activation and crystal form reconstruction technology to realize the complete resource utilization with high added value of the coal gangue, the production process is green and environment-friendly, no chemical agent is adopted, and the production and preparation method is fully unified with the characteristics of the coal gangue. In the calcining and activating process, a small amount of carbon contained in the coal gangue is fully utilized to generate a heat source, and a hydrothermal structure reforming technology is utilized to carry out crystal form reconstruction on a large amount of inorganic minerals in the activated coal gangue to form the porous adsorption material with high specific surface area. Compared with the prior art, the method has the advantages of simple process, realization of full utilization of the coal gangue resource, product macro particle size of 10-20 microns, nano-porous form of the micro secondary structure, pore size of 2-15 nanometers, nano-micron multilevel structure and easy realization of industrial production.|DRAWINGS DESCRIPTION|[0016] FIG. 1 is a scanning electron microscope image of the coal gangue adsorption material prepared in example 2.|[0017] As can be seen from FIG. 1a, the coal gangue adsorbent material prepared in example 2 is a spherical particle with a diameter of about 15 μm, and as can be seen from FIG. 1B, the spherical particle is composed of a stack of nano-scale plate-like and nano-scale spherical particles.|[0018] FIG. 2 is a pore structure distribution diagram of the coal gangue adsorbent prepared in example 3.|[0019] As can be seen from FIG. 2, the size peak values of the pores of the coal gangue adsorbent prepared in example 3 are 5nm and 10 nm.|INVENTION MODE|[0020] Detailed Description|[0021] The invention will be further described with reference to the following examples:|[0022] the invention adopts the comprehensive treatment technology of micronization, calcination decarbonization activation and hydrothermal structure regulation, does not adopt chemical agents, does not generate secondary waste and has simple process. Firstly, mechanically crushing to prepare coal gangue micropowder; then calcining the coal gangue micro powder to remove carbon in the coal gangue micro powder, performing auxiliary calcination by using the carbon contained in the coal gangue as fuel to activate inorganic components in the coal gangue, and performing hydrothermal structure regulation treatment to enable the coal gangue micro powder to form a nano-scale porous structure to obtain the coal gangue micro powder with the diameter of 10-20 microns and the specific surface area of 200-320m2The coal gangue micro powder particles are internally provided with rich-level micropore and mesopore structures, the pore structures are developed, the specific surface area is large, the coal gangue micro powder particles are of nano-level structures, the coal gangue micro powder particles have good adsorption and removal effects on organic dyes and heavy metal ions in polluted wastewater, the pore volume reaches 0.4-0.7cm3/g, and the pore diameter is 2-15 nm.|[0023] Example 1:|[0024] a1, preparation of coal gangue powder: crushing the coal gangue to 5 mm in average particle size by using a jaw crusher, and then processing by using a ball mill to obtain coal gangue powder with particle size less than 45 microns;|[0025] a2, calcining for decarbonization and activating treatment: calcining the coal gangue powder obtained from A1 at the high temperature of 600 ℃, preserving the heat for 2 hours, and naturally cooling to obtain calcined decarbonized activated coal gangue powder;|[0026] a3, mixing the calcined coal gangue powder obtained in A2 with water for pulping, wherein the mass ratio of the calcined coal gangue powder to the water is 1: 4; and then stirring and reacting in a reaction kettle for 48 hours at 180 ℃, cooling, performing solid-liquid separation by using a centrifugal machine, drying and grinding to finally prepare the coal gangue adsorption material for water treatment.|[0027] Example 2:|[0028] a1, preparation of coal gangue powder: crushing the coal gangue to a median particle size of 5 mm by using a jaw hammer crusher, and then processing by using a ring roller mill to obtain coal gangue powder with a particle size of less than 72 microns;|[0029] a2, calcining to remove carbon, and activating: calcining the coal gangue powder obtained from A1 at a high temperature of 700 ℃, preserving the heat for 2 hours, and naturally cooling to obtain calcined coal gangue powder;|[0030] a3, mixing the calcined coal gangue powder obtained in A2 with water for pulping, wherein the mass ratio of the calcined coal gangue powder to the water is 1: 6; and then stirring and reacting in a pressure reaction kettle at the temperature of 200 ℃ for 12 hours, cooling, performing solid-liquid separation by adopting a centrifugal machine, drying and grinding to finally prepare the coal gangue adsorption material for water treatment.|[0031] Example 3:|[0032] a1, preparation of coal gangue powder: crushing the coal gangue by using a jaw crusher until the average grain diameter is 5 mm, and then processing by using a ball mill to obtain coal gangue powder with the average grain diameter less than 45 microns;|[0033] a2, calcining and activating treatment: calcining the gangue powder obtained from A1 at the high temperature of 550 ℃, preserving the heat for 2 hours, and naturally cooling to obtain calcined coal gangue;|[0034] a3, mixing the calcined coal gangue powder obtained in the step A2 with water for pulping, wherein the mass ratio of the calcined coal gangue to the water is 1: 10; and then stirring and reacting in a pressure reaction kettle for 16 hours at 220 ℃, cooling, performing solid-liquid separation by using a centrifugal machine, drying and grinding to finally prepare the coal gangue adsorption material. (CN112246215)|TECHNICAL FIELD|[0002] The invention relates to the technical field of solid waste resource utilization and material preparation, in particular to a method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material.|BACKGROUND ART|[0004] The coal gangue is solid waste in the coal washing and selecting process, and the main components of the coal gangue are silicate minerals and a small amount of coal carbon. At present, the resource utilization approach of the coal gangue mainly comprises coal gangue power generation, but only the coal gangue with higher calorific value can be utilized, and a large amount of generated waste residues need to be further treated; the coal gangue is used as a building auxiliary material for paving, cement doping, brick making and the like, but has low additional value and high transportation cost and can only be utilized nearby. Some methods adopt gravity separation and flotation to extract kaolinite, pyrite and the like in the ore with certain mineral content reaching certain grade. In some researches, chemical treatment of coal gangue is adopted, aluminum chloride is prepared to serve as a water treatment agent, strong acid and strong alkali are adopted in the preparation process for leaching treatment, certain environmental hazards are caused, and a large amount of leaching residual waste residues are generated.|[0005] Disclosure of Invention|[0006] The invention aims to provide a method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material aiming at the defects in the prior coal gangue utilization technology. The invention completely does not use chemical agents, and prepares a novel coal gangue adsorption purification material with a nano-level porous structure by taking coal gangue as a raw material. The preparation method is environment-friendly, the coal gangue is completely converted into the adsorption water purification material, and no secondary waste is generated in the preparation process.|[0007] The object of the invention can be achieved by the following technical measures:|[0008] the method for preparing the adsorbing material for water treatment by using the coal gangue as the raw material comprises the following steps:|[0009] a1, coal gangue micronization treatment: crushing the massive coal gangue into coal gangue powder with the granularity less than 45 microns by adopting mechanical crushing;|[0010] a2, calcining to remove carbon, and activating: calcining the coal gangue powder obtained in the step A1 at the high temperature of 500-800 ℃, keeping the temperature for 60-180 minutes, and naturally cooling to obtain calcined coal gangue powder;|[0011] a3, mixing the calcined coal gangue powder obtained in the step A2 with water to prepare slurry, wherein the mass ratio of the calcined coal gangue powder to the water is 1: 3-10; and then stirring and reacting in a pressure reaction kettle at the temperature of 180-250 ℃ for 12-48 hours, cooling, performing solid-liquid separation by using a centrifugal machine, drying, and grinding to finally prepare the coal gangue adsorbing material for water treatment.|[0012] The coal gangue adsorption material for water treatment has the diameter of 10-20 microns and the specific surface area of 200-320m2The coal gangue micro powder particles have rich hierarchical porous structures, the pore volume of the coal gangue micro powder particles reaches 0.4-0.7cm3/g, and the pore diameter is 2-15 nm.|[0013] The invention has the following beneficial effects:|[0014] the invention adopts the calcining activation and crystal form reconstruction technology to realize the complete resource utilization with high added value of the coal gangue, the production process is green and environment-friendly, no chemical agent is adopted, and the production and preparation method is fully unified with the characteristics of the coal gangue. In the calcining and activating process, a small amount of carbon contained in the coal gangue is fully utilized to generate a heat source, and a hydrothermal structure reforming technology is utilized to carry out crystal form reconstruction on a large amount of inorganic minerals in the activated coal gangue to form the porous adsorption material with high specific surface area. Compared with the prior art, the method has the advantages of simple process, realization of full utilization of the coal gangue resource, product macro particle size of 10-20 microns, nano-porous form of the micro secondary structure, pore size of 2-15 nanometers, nano-micron multilevel structure and easy realization of industrial production.|DRAWINGS DESCRIPTION|[0016] FIG. 1 is a scanning electron microscope image of the coal gangue adsorption material prepared in example 2.|[0017] As can be seen from FIG. 1a, the coal gangue adsorbent material prepared in example 2 is a spherical particle with a diameter of about 15 μm, and as can be seen from FIG. 1B, the spherical particle is composed of a stack of nano-scale plate-like and nano-scale spherical particles.|[0018] FIG. 2 is a pore structure distribution diagram of the coal gangue adsorbent prepared in example 3.|[0019] As can be seen from FIG. 2, the size peak values of the pores of the coal gangue adsorbent prepared in example 3 are 5nm and 10 nm.|INVENTION MODE|[0020] Detailed Description|[0021] The invention will be further described with reference to the following examples:|[0022] the invention adopts the comprehensive treatment technology of micronization, calcination decarbonization activation and hydrothermal structure regulation, does not adopt chemical agents, does not generate secondary waste and has simple process. Firstly, mechanically crushing to prepare coal gangue micropowder; then calcining the coal gangue micro powder to remove carbon in the coal gangue micro powder, performing auxiliary calcination by using the carbon contained in the coal gangue as fuel to activate inorganic components in the coal gangue, and performing hydrothermal structure regulation treatment to enable the coal gangue micro powder to form a nano-scale porous structure to obtain the coal gangue micro powder with the diameter of 10-20 microns and the specific surface area of 200-320m2The coal gangue micro powder particles are internally provided with rich-level micropore and mesopore structures, the pore structures are developed, the specific surface area is large, the coal gangue micro powder particles are of nano-level structures, the coal gangue micro powder particles have good adsorption and removal effects on organic dyes and heavy metal ions in polluted wastewater, the pore volume reaches 0.4-0.7cm3/g, and the pore diameter is 2-15 nm.|[0023] Example 1:|[0024] a1, preparation of coal gangue powder: crushing the coal gangue to 5 mm in average particle size by using a jaw crusher, and then processing by using a ball mill to obtain coal gangue powder with particle size less than 45 microns;|[0025] a2, calcining for decarbonization and activating treatment: calcining the coal gangue powder obtained from A1 at the high temperature of 600 ℃, preserving the heat for 2 hours, and naturally cooling to obtain calcined decarbonized activated coal gangue powder;|[0026] a3, mixing the calcined coal gangue powder obtained in A2 with water for pulping, wherein the mass ratio of the calcined coal gangue powder to the water is 1: 4; and then stirring and reacting in a reaction kettle for 48 hours at 180 ℃, cooling, performing solid-liquid separation by using a centrifugal machine, drying and grinding to finally prepare the coal gangue adsorption material for water treatment.|[0027] Example 2:|[0028] a1, preparation of coal gangue powder: crushing the coal gangue to a median particle size of 5 mm by using a jaw hammer crusher, and then processing by using a ring roller mill to obtain coal gangue powder with a particle size of less than 72 microns;|[0029] a2, calcining to remove carbon, and activating: calcining the coal gangue powder obtained from A1 at a high temperature of 700 ℃, preserving the heat for 2 hours, and naturally cooling to obtain calcined coal gangue powder;|[0030] a3, mixing the calcined coal gangue powder obtained in A2 with water for pulping, wherein the mass ratio of the calcined coal gangue powder to the water is 1: 6; and then stirring and reacting in a pressure reaction kettle at the temperature of 200 ℃ for 12 hours, cooling, performing solid-liquid separation by adopting a centrifugal machine, drying and grinding to finally prepare the coal gangue adsorption material for water treatment.|[0031] Example 3:|[0032] a1, preparation of coal gangue powder: crushing the coal gangue by using a jaw crusher until the average grain diameter is 5 mm, and then processing by using a ball mill to obtain coal gangue powder with the average grain diameter less than 45 microns;|[0033] a2, calcining and activating treatment: calcining the gangue powder obtained from A1 at the high temperature of 550 ℃, preserving the heat for 2 hours, and naturally cooling to obtain calcined coal gangue;|[0034] a3, mixing the calcined coal gangue powder obtained in the step A2 with water for pulping, wherein the mass ratio of the calcined coal gangue to the water is 1: 10; and then stirring and reacting in a pressure reaction kettle for 16 hours at 220 ℃, cooling, performing solid-liquid separation by using a centrifugal machine, drying and grinding to finally prepare the coal gangue adsorption material. Family Number|(92402840)|92402840|Abstract|(CN112246215 A)|A method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material is characterized by comprising the following steps : A1 , coal gangue micronization treatment : crushing blocky coal gangue into coal gangue powder with the particle size of less than 45 microns by adopting mechanical crushing ; A2 , calcining carbon removal and activation treatment : calcining the coal gangue powder obtained in the step A1 at a high temperature of 500800 DEG C , keeping the temperature for 60180 minutes , and naturally cooling to obtain calcined coal gangue powder ; A3 , mixing thecalcined coal gangue powder obtained in the step A2 with water to prepare slurry , wherein the mass ratio of the calcined coal gangue powder to the water is 1 : ( 3-10 ) ; then performing stirring and reacting for 12-48 hours in a pressure reaction kettle at 180-250 DEG C , cooling , then carrying out solid - liquid separation by adopting a centrifugal machine , and then performing drying and grinding to finally obtain the coal gangue adsorbing material for water treatment . |CPC codes|(CN112246215 A)|B01J - 020/10 |B01J - 020/28/021 |IPC codes|(CN112246215 A)|B01J - 020/10 |B01J - 020/28 | Chemical engineering|Environmental technology B01J-020/10|B01J-020/28/021|C02F-001/28/1|C02F-2101/20|C02F-2101/308 B01J-020/10|B01J-020/28/021|C02F-001/28/1|C02F-2101/20|C02F-2101/308 B01J-020/10|B01J-020/28|C02F-001/28|C02F-101/20|C02F-101/30 B01J-020/10|B01J-020/28|C02F-001/28|C02F-101/20|C02F-101/30 CN116440854|CN115025756|CN120005632B|CN116694334B CN116440854 105777692 WHO=Examiner SELF=N CAT=A|CN115025756 101696191 WHO=Examiner SELF=N CAT=A|CN120005632B 114610095 WHO=Examiner SELF=N|CN116694334B 106360199 WHO=Examiner SELF=N WO2019147664|CN109336125|KR20200071177|CN106975440|CN106517224|CN103386294|CN101274267|JP2003126848 WO2019147664 85539905 WHO=Examiner SELF=N CAT=A|CN109336125 83399158 WHO=Examiner SELF=Y CAT=A|KR20200071177 89319652 WHO=Examiner SELF=N CAT=A|CN106975440 76825853 WHO=Examiner SELF=N CAT=A|CN106517224 75716073 WHO=Examiner SELF=N CAT=A|CN103386294 59333403 WHO=Examiner SELF=N CAT=A|CN101274267 6614196 WHO=Examiner SELF=Y CAT=A|JP2003126848 31809828 WHO=Examiner SELF=N CAT=A 乌锡康: &quot;《有机化工废水治理技术》&quot;, 31 July 1999, 化学工业出版社, pages: 347 (Cat. A)|商平等: &quot;《环境矿物材料》&quot;, 31 January 2008, 化学工业出版社, pages: 135 (Cat. A)|李尉卿等: &quot;煤矸石活化制作吸附材料的初步研究&quot;, 《环境工程》, vol. 22, no. 1, 29 February 2004 (2004-02-29) (Cat. Y) JP2003126848; CN101274267; CN103386294; CN106517224; CN106975440; CN109336125; WO2019147664; KR20200071177 LAPSED (CN112246215)|LAPSED DEAD (CN112246215)|DEAD (CN112246215)|LEGAL DETAILS FOR CN112246215|Actual or expected expiration date=2023-03-10|Legal state=DEAD|Status=LAPSED|Event publication date=2020-11-04|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202011213586|Application date=2020-11-04|Standardized application number=2020CN-1213586|Event publication date=2021-01-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN112246215|Publication stage code=A|Publication date=2021-01-22|Standardized publication number=CN112246215|Event publication date=2021-01-22|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2021-02-09|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-03-10|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQ6yU7kXm8HrFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000055585758&ekey=2009&xpn=CN112246215&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=j1TIk3svcVswGpZWUeB5ZpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN112246215)|CN (CN112246215)|NAME=HENAN POLYTECHNIC UNIVERSITY , COUNTRY=CN (CN112246215)|NAME=GUO ZHONGMIN;ZHENGZHOU ZHONGMIN PATENT AGENT CO., LTD , REG=41110 (CN112246215)|NAME=ZHANG QIAN|NAME=ZHANG YUDE|NAME=CHEN ZIYI|NAME=YIN SHUAIJUN|NAME=KANG YAMIN|NAME=ZHAO XIAOLEI|NAME=FENG ZHAOXIANG 0 1 Titre: (CN112246215)|Method for preparing adsorbing material for water treatment by taking coal gangue as raw material Résumé: (CN112246215)|A method for preparing an adsorbing material for water treatment by taking coal gangue as a raw material is characterized by comprising the following steps: A1, coal gangue micronization treatment: crushing blocky coal gangue into coal gangue powder with the particle size of less than 45 microns by adopting mechanical crushing; A2, calcining carbon removal and activation treatment: calcining the coal gangue powder obtained in the step A1 at a high temperature of 500800 DEG C, keeping the temperature for 60180 minutes, and naturally cooling to obtain calcined coal gangue powder; A3, mixing thecalcined coal gangue powder obtained in the step A2 with water to prepare slurry, wherein the mass ratio of the calcined coal gangue powder to the water is 1: (3-10); then performing stirring and reacting for 12-48 hours in a pressure reaction kettle at 180-250 DEG C, cooling, then carrying out solid-liquid separation by adopting a centrifugal machine, and then performing drying and grinding to finally obtain the coal gangue adsorbing material for water treatment. 73 Abstract gpt-4o-mini no The article focuses on preparing an adsorbing material for water treatment using coal gangue, which does not relate to accelerated weathering or CO₂ capture.
74 CN202511686192 CN202511686192 CN121176213 117150097 CN121176213 A 2025-12-23 [CN121176213] 2025-11-18 2025-11-18 2025-12-23 (CN121176213)|2045-11-18 (CN121176213)|Tea garden soil organic carbon improving method based on deep ploughing and trimmed object returning to field (CN121176213)|The invention provides a tea garden soil organic carbon improving method based on deep ploughing and trimmed object returning, and relates to the technical field of soil remediation. The tea garden soil organic carbon improving method based on deep ploughing and trimmed object returning comprises the following steps that S1, tea garden soil is layered, the soil is deeply ploughed to 80-100 cm, and a soil layer is divided into a soil surface layer and a soil deep layer; s2, pruning tea trees after tea picking, and crushing pruned objects to 2-5 cm to obtain pruned object fragments; s3, applying compound fertilizer to the surface layer of the soil, and applying the trimmed object fragments and organic fertilizer in the step S2 to the deep layer of the soil; s4, performing water management on the soil through micro-spray irrigation to improve organic carbon in the soil of the tea garden. According to the method, deep ploughing and returning of pruned objects to the field are combined, the carbon sequestration capacity of the tea garden soil is remarkably improved, the deep SOC mineralization rate is reduced, the residence time of carbon in the soil is prolonged, the overall carbon sequestration efficiency is improved, the microbial community structure is optimized, the gene abundance related to carbon decomposition in the deep soil is reduced, and the resource utilization rate is increased. TEA RESEARCH INSTITUTE CHINESE ACADEMY OF AGRICULTURAL SCIENCES (CN121176213)|TEA RESEARCH INSTITUTE CHINESE ACADEMY OF AGRICULTURAL SCIENCES ([CN]) ZHANG SHAOBO|LI XIN|ZHANG LAN|YAN PENG|ZHANG HONGBIN|HUANG SHUPING (CN121176213)|ZHANG SHAOBO|LI XIN|ZHANG LAN|YAN PENG|ZHANG HONGBIN|HUANG SHUPING (CN121176213)|ZHANG XU;BEIJING XINRUISEN INTELLECTUAL PROPERTY AGENCY CO., LTD.|Reg. Nb: 11961 (CN121176213)|In contrast, deep soil (below 40 cm) has the natural advantage of low mineralization rate, but the carbon fixation potential is not effectively developed and utilized for a long time due to insufficient carbon input.|Although studies have revealed that tea tree pruning returns to the field to improve soil fertility and carbon storage, the prior art is still limited to traditional surface layer applications and fails to achieve directional migration of carbon sources into deep soil.|First is the problem of carbon cycle imbalance. The existing management measures are concentrated on surface soil (0-20 cm), and the organic carbon content of the soil can be improved in a short period of time when the pruning is returned to the field, but the decomposition rate of the organic carbon is too high due to high activity of microorganisms and enzymes in the surface soil, so that long-term solid storage is difficult to realize.|The existing cultivation mode has obvious limitation on the regulation and control of soil microbial communities, particularly the cognitive insufficiency of functional microbial communities on deep soil, the effective regulation and control of soil organic carbon mineralization inhibition bacterial communities are difficult, and an effective soil organic carbon protection mechanism cannot be established.| (CN121176213)|1. The tea garden soil organic carbon lifting method based on deep turning and pruning returning is characterized by comprising the following steps of: S1, layering the soil of a tea garden, deeply turning the soil to 80-100 cm, and dividing the soil layer into a soil surface layer and a soil deep layer; S2, pruning tea trees after picking tea, and crushing the prunes to 2-5 cm to obtain prune fragments; s3, applying a compound fertilizer to the surface layer of the soil, and applying the pruning fragments and the organic fertilizer in the S2 to the deep layer of the soil; S4, carrying out water management on the soil through micro-spray irrigation, and improving organic carbon in the tea garden soil. | (CN121176213)|In order to solve the problems, the invention provides a tea garden soil organic carbon lifting method based on deep turning and pruning to return to the field.|The invention provides a tea garden soil organic carbon lifting method based on deep ploughing and pruning returning, and relates to the technical field of soil restoration. The invention discloses a tea garden soil organic carbon lifting method based on deep-turning and pruning and returning, which comprises the following steps of S1 layering tea garden soil, deep-turning the soil to 80-100 cm, dividing the soil layer into a soil surface layer and a soil deep layer, S2 pruning tea trees after tea picking, crushing the pruning to 2-5 cm to obtain pruning fragments, S3 applying a compound fertilizer on the soil surface layer, applying the pruning fragments and organic fertilizers in S2 on the soil deep layer, and S4 performing moisture management on the soil through micro-spray irrigation to lift the tea garden soil organic carbon.|The invention relates to the technical field of soil remediation, in particular to a tea garden soil organic carbon lifting method based on deep ploughing and pruning returning.| (CN121176213)|TEA GARDEN SOIL(100,22)|DEEP TURNING(100,13)|SOIL ORGANIC CARBON(100,13)|TEA(100,12)|SOIL ORGANIC CARBON LIFTING(100,2)|PRUNING RETURNING(100,1)|TEA GARDEN(82,14)|PRUNING FRAGMENT(74,3)|MINERALIZATION INHIBITION BACTERIAL COMMUNITY(72,1)|PRUNING TEA TREE(60,4)|INSUFFICIENCY COGNITION(58,1)|FERTILIZER COMPOUND(55,8)|LAND RESTORATION(55,1)|PRUNING(54,21)|TEA PICKING(53,1)|DEEP PLOWING(45,16)|MOISTURE MANAGEMENT(45,1)|SOIL MICROBIAL COMMUNITY(45,1)|SOIL DEPTH(41,31)|LIFTING(41,6)|CHINESE VEGETABLE SEED CAKE(41,1)|MIGRATION DIRECTION(41,1)|GROUND(39,40)|LAYERING TEA(39,3)|MICROBIAL COMMUNITY FUNCTION(37,1)|PICKING TEA(35,3)|IRRIGATION(34,3)|REGULATION(34,2)|MICROSPRINKLING IRRIGATION(33,3)|SOIL DEEP LAYER(30,8)|LIFTING ORGANIC CARBON(30,6)|FRAGMENT(29,3)|CULTIVATION MODE(27,1)|GROUND LAYER(26,41)|GENE ABUNDANCE(26,6)|RAPESEED CAKE(25,3)|TEA CARBON FIXATION CAPACITY(25,1)|NITROGEN PHOSPHORUS POTASSIUM FERTILIZER(23,4)|MANAGEMENT MEASURE(23,2)|CARBON DECOMPOSITION(23,1)|SOIL REMEDIATION(23,1)|ORGANIC FERTILIZER(22,17)|MINERALIZATION RATE(22,2)|SOIL FERTILITY(21,1)|PRUNE(20,3)|CARBON CYCLE IMBALANCE(20,1)|CARBON FIXATION POTENTIAL(20,1)|DEEP SOC(19,2)|MICROORGANISM(19,2)|CARBON SOURCE DIRECTIONAL MIGRATION(18,1)|INSUFFICIENT CARBON INPUT(17,2)|CARBON STORAGE(17,1)|DECOMPOSITION(16,3)|FARMYARD MANURE(16,2)|CARBON FIXATION(15,24)|TEA GARDEN ECOSYSTEM(15,2)|ORGANIC CARBON(13,16)|CBHI ABUNDANCE(13,3)|ENZYME(12,3)|WATER MANAGEMENT(12,1)|TEA TREE(11,7)|MICROBIAL BIOMASS CARBON(11,3)|NANODROP ND 1000 SPECTROPHOTOMETER(11,1)|ZONAL FERTILIZATION STRATEGY(11,1)|CELLOBIOHYDROLASE(10,8)|GROUND SURFACE LAYER(10,5)|MICROBIAL COMMUNITY REGULATION(10,3)|ORGANIC CARBON CONTENT(10,2)|RESOURCE UTILIZATION RATE(10,2)|DIFFERENTIATED FERTILIZATION STRATEGY(10,1)|PROTECTION(10,1)|PRUNED FRAGMENT MIGRATION(10,1)|PRUNING RESIDUE FERTILIZATION(10,1)|TEA GARDEN ECOLOGICAL BENEFIT(10,1)|MICROBIAL COMMUNITY STRUCTURE(9,5)|MICROORGANISM UTILIZATION(9,2)|ARMORED COCCI CLASS(9,1)|CENTURY CULTIVATION HISTORY(9,1)|DEEP HYPERSALINITY FLORA(9,1)|DEEP PLOWING CULTIVATION ADOPTION(9,1)|SOIL MICROORGANISM BIOMASS(9,1)|ELEMENTAL ANALYZER(8,2)|EMISSION DYNAMICS(8,2)|FUNGAL COLONY(8,2)|PARTITION MANAGER(8,2)|PRUNE FRAGMENT(8,2)|SAMPLING DESTRUCTION(8,2)|TECHNICAL BOTTLE NECK(8,2)|CORE TECHNOLOGY BREAKTHROUGH(8,1)|DEEP SOIL MINERALIZATION(8,1)|FUNCTIONAL MICROORGANISM ABUNDANCE(8,1)|HYPERSALINITY BACTERIUM(8,1)|MICROORGANISM REGULATION DEFECT(8,1)|MINERALIZATION FUNCTIONAL FLORA(8,1)|TEA GARDEN ACCURATE MANAGEMENT(8,1)|SURFACE LAYER(7,9)|DEEP TURNING DEPTH(7,4)|CARBON CYCLE(7,2)|REGULATION DIRECTION(7,2)|515F 806R PRIMER(7,1)|DEEP SOIL MICROECOLOGICAL ENVIRONMENT(7,1)|DIRECTIONAL DEEP BURYING(7,1)|DOTHIDEOMYCETE MICROBIAL COMMUNITY(7,1)|ITS3F ITS4R PRIMER(7,1)|LONGJING TEA ANNUAL YIELD(7,1)|MORTIERELLA ABUNDANCE(7,1)|SORDARIOMYCETE MICROBIAL COMMUNITY(7,1)|TAXONOMIC ANNOTATION(7,1)|URFACE HYPERSALINITY(7,1)|DEEP LAYER(6,8)|BACTERIAL COLONY(6,2)|DECREASE TREND(6,2)|DECREASING TREND(6,2)|MICROBIAL COMMUNITY SYNERGISTIC CHANGE(6,2)|MOISTURE REGULATION(6,2)|WET SIEVING(6,2)|1M TRISHCL BUFFER(6,1)|ABI GENEAMP(6,1)|BACTERIAL COMMUNITY(6,1)|BOTTLE HEADSPACE(6,1)|CBHI GENE MARKER(6,1)|CHLOROFORM FUMIGATION POTASSIUM SULFATE(6,1)|CIRCULATION FUNCTIONAL FLORA(6,1)|DEEP FUNCTIONAL MICROFLORA(6,1)|DEEP SOIL BETA GLUCOSIDASE(6,1)|DEEP SOIL MBC CONTENT(6,1)|DEEP SOIL NECESSITY(6,1)|FUNGAL COMMUNITY(6,1)|MAJOR WORLD BEVERAGE(6,1)|MICROBIAL COMMUNITY SUCCESSION(6,1)|MINERALIZATION INHIBITION(6,1)|MINERALIZATION ZONE(6,1)|OMEGA PURIFICATION KIT(6,1)|SOC MINERALIZATION(6,1)|SOIL DEPTH LAYERING(6,1)|TRANSSTARTFASTPFU DNA POLYMERASE(6,1)|TREMELLA BACTERIUM(6,1)|SURFACE SOIL(5,4)|CENTRIFUGATION(5,3)|DEEP CARBON FIXATION(5,3)|DECOMPOSITION RATE BALANCE(5,2)|DEEP SOIL CARBON FIXATION(5,2)|GENE MARKER FUNCTION(5,2)|SLOW DECOMPOSITION(5,2)|SOC BREAKDOWN RATE(5,2)|5M CACL(5,1)|AMPLICON SEQUENCE VARIANT(5,1)|ANNUAL PRECIPITATION(5,1)|BACTERIAL 16S RIBOSOMAL RNA(5,1)|BASE FERTILIZER DEEP FERTILIZATION(5,1)|CO2 QUANTIFICATION(5,1)|CULTURE EXPERIMENT(5,1)|DEEP FUNCTIONAL MICROORGANISM(5,1)|DEEP HYPOALINITY(5,1)|DEEP MICROBIAL COMMUNITY(5,1)|EAST LONGITUDE(5,1)|INSUFFICIENT CULTIVATION DEPTH(5,1)|LAYERED ACCURATE MANAGEMENT(5,1)|MANAGEMENT REGION(5,1)|MICROBIAL REGULATION(5,1)|MICROPOROUS FILTER MEMBRANE(5,1)|NORTH LATITUDE(5,1)|PRUNED SOIL(5,1)|SCIENTIFIC PLANTING(5,1)|SEQUENCE LIBRARY(5,1)|SPRING TEA ANNUAL YIELD(5,1)|TOC ANALYZER(5,1)|UNBALANCED CARBON CIRCULATION(5,1)|CARBON SOURCE(4,8)|GROUND LAYER DEPTH(4,3)|DNA EXTRACTION(4,2)|FERTILIZER UTILIZATION RATE(4,2)|MINERAL BINDING ORGANIC CARBON(4,2)|NUTRIENT(4,2)|PARTICLE DIAMETER(4,2)|BIOINFORMATICS ANALYSIS(4,1)|BLANK CONTAINER(4,1)|CBHI GENE EXPRESSION(4,1)|CULTURE VESSEL(4,1)|DINITROSALICYLIC ACID(4,1)|ECOLOGICAL SAFETY(4,1)|ECOLOGICAL TARGET(4,1)|ECONOMIC BENEFIT(4,1)|EXTRACTION KIT(4,1)|FASTQ FORMAT(4,1)|FECAL CRUSTACEAN RELATIVE ABUNDANCE(4,1)|FILTERING SUPERNATANT(4,1)|GENE REGION AMPLIFICATION(4,1)|GROUND MINERAL(4,1)|GROUPING SEPARATION(4,1)|GUARANTEED QUALITY(4,1)|LAYER SURFACE SOIL(4,1)|LOAM CLAY(4,1)|LONG TERM SOLID STORAGE(4,1)|MINERALIZATION FLORA RELATIVE ABUNDANCE(4,1)|PLUM HOME(4,1)|POC SEPARATION(4,1)|PURIFIED DNA SAMPLE(4,1)|SOIL SUSPENSION(4,1)|SUBSURFACE LAYER BETA GLUCOSIDASE(4,1)|TEA DEPTH(4,1)|TEA GARDEN WASTE(4,1)|TEA ORGANIC CARBON MINERALIZATION(4,1)|TEA TARGETED CARBON MANAGEMENT(4,1)|TECHNICAL SYNERGY(4,1)|TOO RAPID MINERALIZATION(4,1)|TRIMMING TRACK(4,1)|WESTERN LAKE REGION(4,1)|SOIL SAMPLE(3,4)|WATER CONTENT(3,3)|ABSORPTION VESSEL(3,1)|ABUNDANCE DISTRIBUTION RULE(3,1)|CARBON CIRCULATION DIFFERENCE(3,1)|CARBON DEGRADATION(3,1)|CARBON METABOLISM(3,1)|CARBON STARVATION(3,1)|CLUSTER DISTRIBUTION(3,1)|COLONIZATION(3,1)|CONTAINED MAOC(3,1)|CUMULATIVE RELEASE(3,1)|DECOMPOSABLE CARBON COMPONENT(3,1)|DEEP MICROORGANISM FUNCTION(3,1)|DEEP PLOWING DEPTH(3,1)|DEEP TURNING TREATMENT(3,1)|DEPTH GRADIENT(3,1)|DISTINCTION(3,1)|DIVERSITY(3,1)|FERTILIZATION MODE(3,1)|HUMID SUBTROPICAL CLIMATE(3,1)|KEY FLORA(3,1)|LEACHING SOLUTION(3,1)|MODIFIED UNIVERSAL BUFFER(3,1)|MOLECULAR ANALYSIS(3,1)|MORTIERELLOMYCETE(3,1)|NAOH ABSORPTION SOLUTION(3,1)|ORGANIC CARBON INHIBITING MINERALIZATION(3,1)|ORGANIC CARBON RESERVE ACCUMULATION(3,1)|PCR REACTION(3,1)|POC COMPONENT(3,1)|POC CONTENT(3,1)|POC REMOVAL(3,1)|POTASSIUM COMPOUND FERTILIZER(3,1)|PREDENATURATION(3,1)|SEQUENCE AMPLIFICATION(3,1)|SOC DECOMPOSITION RATE(3,1)|STATISTICAL DIFFERENCE(3,1)|SYNERGISTIC ACTION(3,1)|TEA CARBON FIXING CAPABILITY(3,1)|TEA PLANT GROWTH(3,1)|TEA STABLE YIELD(3,1)|TEA YIELD(3,1)|TECHNICAL FEASIBILITY BALANCE(3,1)|TREMELLOMYCETE(3,1)| (CN121176213)|1. The tea garden soil organic carbon lifting method based on deep turning and pruning returning is characterized by comprising the following steps of:| S1, layering the soil of a tea garden, deeply turning the soil to 80-100 cm, and dividing the soil layer into a soil surface layer and a soil deep layer; | S2, pruning tea trees after picking tea, and crushing the prunes to 2-5 cm to obtain prune fragments; | s3, applying a compound fertilizer to the surface layer of the soil, and applying the pruning fragments and the organic fertilizer in the S2 to the deep layer of the soil; | S4, carrying out water management on the soil through micro-spray irrigation, and improving organic carbon in the tea garden soil. |2. The method for lifting organic carbon in tea garden soil based on deep ploughing and pruning in field according to claim 1, wherein the depth of the soil surface layer in the step S1 is 0-40 cm, and the depth of the soil deep layer is 40-100 cm.|3. The method for improving organic carbon in tea garden soil based on deep ploughing and pruning in field according to claim 1, wherein in the step S3, the compound fertilizer is a nitrogen-phosphorus-potassium fertilizer.|4. The method for improving organic carbon in tea garden soil based on deep ploughing and pruning according to claim 3, wherein in the step S3, the N: P: k=3:1:1 of the nitrogen-phosphorus-potassium fertilizer.|5. The method for lifting organic carbon in tea garden soil based on deep ploughing and pruning in the field according to claim 1, wherein in the step S3, the nitrogen application amount of the compound fertilizer is 450-480 kg N/ha.|6. The method for lifting organic carbon in tea garden soil based on deep turning and returning of trimmings according to claim 1, wherein in the step S3, the application amount of the trimmings is 2800-3200 kg/ha.|7. The method for lifting organic carbon in tea garden soil based on deep turning and pruning as well as returning to field according to claim 1, wherein in the step S3, the application amount of the organic fertilizer is 5700-6300 kg/ha.|8. The method for lifting organic carbon in tea garden soil based on deep ploughing and trimming to field according to claim 1, wherein in the step S3, the organic fertilizer comprises rapeseed cake and farmyard manure.|9. The method for lifting organic carbon in tea garden soil based on deep ploughing and trimming to field according to claim 8, wherein in the step S3, the proportion of the Chinese vegetable seed cake is more than or equal to 80wt.%, and the C/N ratio is (20-25): 1.|10. The method for improving organic carbon in tea garden soil based on deep ploughing and returning of pruning to field according to claim 1, wherein in the step S4, the water content of the soil after micro-sprinkling irrigation is 55% -65%. (CN121176213)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of soil remediation, in particular to a tea garden soil organic carbon lifting method based on deep ploughing and pruning returning.|BACKGROUND ART|[0002] Tea leaves are one of three major world beverages, and main chemical components such as catechin, caffeine and the like have a plurality of benefits on human health. In modern tea garden management, scientific planting and management are core factors for guaranteeing excellent quality and stable yield of tea. However, the current tea garden soil organic carbon lifting technology mainly has three technical bottlenecks.|[0003] First is the problem of carbon cycle imbalance. The existing management measures are concentrated on surface soil (0-20 cm), and the organic carbon content of the soil can be improved in a short period of time when the pruning is returned to the field, but the decomposition rate of the organic carbon is too high due to high activity of microorganisms and enzymes in the surface soil, so that long-term solid storage is difficult to realize. In contrast, deep soil (below 40 cm) has the natural advantage of low mineralization rate, but the carbon fixation potential is not effectively developed and utilized for a long time due to insufficient carbon input. And secondly, the defect of microorganism regulation and control. The existing cultivation mode has obvious limitation on the regulation and control of soil microbial communities, particularly the cognitive insufficiency of functional microbial communities on deep soil, the effective regulation and control of soil organic carbon mineralization inhibition bacterial communities are difficult, and an effective soil organic carbon protection mechanism cannot be established. Third is a lack of technical synergy. In the traditional management, all technical links are mutually split, deep-ploughing cultivation is asynchronous with organic carbon supplementation, fertilization strategies are not matched with microbial regulation, a synergistic action chain of carbon input, community regulation and mineralization inhibition cannot be formed, and the continuous accumulation of organic carbon reserves in soil is severely restricted.|[0004] Although studies have revealed that tea tree pruning returns to the field to improve soil fertility and carbon storage, the prior art is still limited to traditional surface layer applications and fails to achieve directional migration of carbon sources into deep soil. Meanwhile, although the conventional cultivation depth (less than or equal to 60 cm) and the fertilization scheme provide 'deep fertilization of base fertilizer', the aim is only to improve the fertilizer utilization rate, and the vertical distinction characteristic of the soil carbon cycle of 'surface hypersalinity and deep hypoalinity' cannot be recognized and utilized, so that the targeted carbon management of the tea garden soil cannot be realized.|DISCLOSURE|Disclosure of Invention|[0005] In order to solve the problems, the invention provides a tea garden soil organic carbon lifting method based on deep turning and pruning to return to the field. According to the invention, through the combination of deep turning and pruning returning, the carbon fixing capability of the tea garden soil is obviously improved, and the residence time of carbon in the soil is prolonged and the overall carbon fixing efficiency is improved by reducing the mineralization rate of deep SOC. Meanwhile, the microbial community structure is optimized, and the gene abundance is increased. And the utilization rate of resources is improved by returning the pruning to the field.|[0006] The invention provides a tea garden soil organic carbon lifting method based on deep ploughing and pruning returning, which specifically comprises the following steps:| s1, layering tea garden soil, deeply turning the soil to 80-100 cm, breaking the original soil structure, but not damaging the root system of tea trees, and dividing the soil layer into a soil surface layer and a soil deep layer; | S2, pruning tea trees after picking tea, and crushing the prunes to 2-5 cm to obtain prune fragments; | s3, applying a compound fertilizer to the surface layer of the soil, and applying the pruning fragments and the organic fertilizer in the S2 to the deep layer of the soil; | s4, carrying out moisture management on the soil through micro-spray irrigation, regulating microbial communities, and improving organic carbon in the soil of the tea garden. |[0007] Preferably, the depth of the soil surface layer in the step S1 is 0-40 cm, and the depth of the soil deep layer is 40-100 cm.|[0008] Preferably, the compound fertilizer in the step S2 is a nitrogen-phosphorus-potassium fertilizer, wherein the N: P: K=3:1:1 of the nitrogen-phosphorus-potassium fertilizer, the nitrogen application amount of the compound fertilizer is 450-480 kg N/ha, the application amount of the pruning is 2800-3200-kg/ha, the application amount of the organic fertilizer is 5700-6300 kg/ha, the organic fertilizer is a rapeseed cake or a mixture of a rapeseed cake and a farmyard manure, the rapeseed cake accounts for more than or equal to 80 wt%, and the C/N ratio is (20-25): 1.|[0009] Preferably, the water content of the soil after micro-sprinkling irrigation in the step S4 is 55% -65%, the water management time is more than or equal to 7 days, and the microbial community regulation comprises the steps of promoting Alphaproteobacteria, sordariomycetes microbial communities and inhibiting Mortierellomycetes, dothideomycetes microbial communities.|[0010] The deep soil is deeply ploughed to 80-100 cm, which is a core technological breakthrough for realizing efficient carbon fixation of tea garden soil, the necessity of the deep soil is derived from the vertical diversity characteristic of organic carbon mineralization of the tea garden soil, the accumulated and released amount of CO 2 of the tea garden soil is obviously reduced along with the depth, the natural low mineralization advantage of the deep soil provides a theoretical basis for long-term carbon fixation, but the premise is that the original compact soil structure is broken through the deep ploughing technology, and an effective physical channel is constructed for migration of a carbon source to the deep layer.|[0011] The traditional tea garden management has obvious technical bottlenecks, which are mainly represented by insufficient cultivation depth and unbalanced carbon circulation. The existing management measures are concentrated on the soil with the surface layer of 0-20 cm, and the pruned soil is quickly decomposed due to the high mineralization rate of the surface layer after returning to the field, so that long-term carbon fixation is difficult to realize. Conventional cultivation depths generally do not exceed 60 cm, and although the concept of deep application of base fertilizer is proposed, the goal is limited to improving fertilizer utilization rate, and the key characteristic of low mineralization of deep soil cannot be recognized and utilized. More importantly, deep soil is in a "carbon starvation" state for a long period of time, and the carbon fixation potential of the deep soil is not effectively exploited. The invention breaks through the depth limit of traditional cultivation by lifting the deep turning depth to 80-100 cm, and establishes a vertical partition management system of 'surface layer yield maintenance and deep carbon fixation' for the first time.|[0012] The depth of less than 70 cm cannot reach the lowest mineralization zone, and the physical channel for downward delivery of the carbon source is blocked, so that the deep soil is still in a state of insufficient carbon input. Meanwhile, the effective root systems of the tea trees are mainly distributed in the range of 0-60 cm, and 80-100 cm are deeply turned below the root systems, so that the soil structure can be broken, the root systems of the tea trees cannot be damaged, and the balance of technical feasibility and ecological safety is realized.|[0013] Deep turning to 80-100 cm creates a necessary condition for the migration of the pruned fragments and organic fertilizer to the deep layer, thereby triggering a series of synergistic carbon fixation mechanisms. Deep ploughing not only delivers a carbon source, but also successfully activates the deep functional microflora. After the deep ploughing and returning the complex pruning material to the field, the activity of beta-glucosidase in deep soil is reduced, the gene abundance of GH48 is reduced, and the activity of cellobiohydrolase is obviously weakened. This mode of microbial control, which "activates but inhibits hypersalinity", is the central mechanism by which deep-turning technology interacts with the trimmings track and field association.|[0014] From the aspect of microbial community structure, the directional regulation and control of key flora is realized by deep turning to 80-100 cm. Although the relative abundance of high mineralization flora such as Mortierellomycetes and Dothideomycetes in deep soil increases with depth, the enrichment of low mineralization functional flora such as Alphaproteobacteria and Sordariomycetes is promoted due to deep ploughing and returning of the pruning object to the field, and simultaneously the activity of carbon degrading enzyme and the expression of functional genes are inhibited, so that the overall mineralization rate is still obviously reduced. The reconstruction of the community structure changes the micro-ecological environment of deep soil by 80-100 cm deep turning, creates favorable conditions for carbon source input, and guides the succession of microbial communities to the direction favorable for carbon fixation.|[0015] In addition, 80-100 cm deep turning is a precondition for realizing layered and accurate management of tea gardens. The compound fertilizer is applied on the surface layer 0-40 cm to maintain the nutrients required by the growth of tea trees and ensure the annual yield of spring tea, and the pruning and organic fertilizer are mixed in the deep layer 40-100 cm to concentrate on long-term carbon fixation. The strategy of upper layer production-protecting and lower layer carbon fixation unifies the production targets and ecological targets which are mutually independent in the past into a set of complete technical scheme. If the deep turning depth is insufficient, the deep soil is still in a state of lack of carbon input, vertical partition management cannot be realized, surface layer trimmings can be mineralized continuously and rapidly, and the deep carbon fixation potential cannot be exerted.|[0016] According to the invention, the carbon fixation efficiency of deep soil is maximized by crushing the pruning to 2-5 cm, the mineralization amount of SOC is improved due to the fact that the specific surface area is too small (2 cm), the deep hypersalinity flora (Mortierellomycetes, dothideomycetes) is triggered to be excessively activated, the activity of beta-glucosidase is obviously improved, a carbon source is rapidly mineralized and released, the mineralization amount of SOC is improved due to slow decomposition and poor contact of soil when the particle size is too large (5 cm), the decomposition carbon component is not provided for deep functional microorganisms (Alphaproteobacteria, sordariomycetes) in time, GH48 and cbhI gene expression is delayed, and the optimal window period for microbial community regulation is missed.|[0017] Compared with the prior art, the invention has the beneficial technical effects that:| Firstly, the deep turning depth is set to 80-100 cm, an effective channel is constructed for the migration of a carbon source to a deep layer, and a zonal fertilization strategy based on the vertical difference of carbon circulation is combined, chemical fertilizers are applied to the surface layer of 0-40 cm to ensure the growth and yield of tea trees, and pruning matters and organic fertilizers are applied in the deep layer of 40-100 cm to successfully activate the functions of deep microorganisms, so that the mineralization rate of organic carbon in the deep layer soil is reduced by 30-49%, and the detention time of carbon in the soil is remarkably prolonged. |[0018] Secondly, the invention optimizes the microbial community structure, promotes the enrichment of Alphaproteobacteria, sordariomycetes and other beneficial bacteria by directional regulation, simultaneously inhibits Mortierellomycetes, dothideomycetes and other hypersalinity bacteria, reduces the beta-glucosidase activity of deep soil by 40% -75%, reduces the GH48 gene abundance by about 20%, and effectively weakens the carbon metabolism function of microorganisms, thereby enhancing the organic carbon fixation capability of soil. In addition, the invention realizes the optimal balance of the decomposition rate and the microorganism utilization efficiency by precisely controlling the particle size of the pruning material (2-5 cm), and avoids the problems of rapid mineralization caused by too small particle size and slow decomposition caused by too large particle size.|[0019] In the aspect of resource utilization, the utilization rate of returning the pruning objects to the field reaches 95%, the input of external organic fertilizer is reduced by about 20%, and the efficient recycling of tea garden waste is realized. More importantly, the invention realizes layered accurate management, adopts a differentiated fertilization strategy aiming at the carbon circulation characteristics of soil with different depths, unifies two previous mutually independent targets of 'upper layer yield-keeping' and 'lower layer carbon fixation' into a complete technical scheme for the first time, maximizes the carbon fixation effect while guaranteeing the tea yield, and realizes the collaborative improvement of the economic benefit and the ecological benefit of the tea garden.|DRAWINGS DESCRIPTION|[0020] The invention is further described with reference to the following description of the drawings.|[0021] FIG. 1 is a process flow diagram of the present invention compared with a conventional method;| fig. 2 is a flow chart of a tea garden deep soil carbon fixation lifting technology in embodiment 1 of the invention; | FIG. 3 is a graph showing the effect of soil layer depth on the accumulated CO 2 emission dynamics of tea garden soil in test example 2 according to the present invention, wherein FIG. 3a is a graph showing the accumulated CO 2 release curves of different soil layer depths, and FIG. 3b is a histogram showing the total CO 2 release amount of each soil layer after 45 days of cultivation; | FIG. 4 is a graph showing the effect of soil layer depth on the abundance of cbhI gene and GH48 gene in tea garden soil in test example 5 of the invention, wherein FIGS. 4a and 4b are the abundance of cbhI gene on day 15 and 45 of culture, respectively, and FIGS. 4c and 4d are the abundance of GH48 gene on day 15 and 45 of culture, respectively; | FIG. 5 is a graph showing the effect of soil layer depth on enzyme activity in tea garden soil in test example 6 of the present invention, wherein FIG. 5a and FIG. 5b are the beta-glucosidase activity on day 15 and day 45 of cultivation, respectively, and FIG. 5c and FIG. 5d are the cellobiohydrolase activity on day 15 and day 45 of cultivation, respectively; | FIG. 6 is a graph showing the effect of soil layer depth on the carbon content of tea garden soil in test example 7 according to the present invention, wherein FIG. 6a and FIG. 6b are POC content on 15 th and 45 th of cultivation, FIG. 6c and FIG. 6d are MAOC content on 15 th and 45 th of cultivation, FIG. 6e and FIG. 6f are WSOC content on 15 th and 45 th of cultivation, respectively, and FIG. 6g and FIG. 6h are MBC content on 15 th and 45 th of cultivation, respectively; | FIG. 7 is a graph showing the composition of bacterial and fungal colonies in tea garden soil at different soil layer depths in test example 8 according to the present invention, wherein FIGS. 7a and 7b are thermal graphs showing the composition of bacterial colonies on 15 th and 45 th of cultivation, respectively, and FIGS. 7c and 7d are thermal graphs showing the composition of fungal colonies on 15 th and 45 th of cultivation, respectively; | FIG. 8 is a schematic diagram showing the mechanism of inhibiting mineralization of organic carbon in soil by synergistic change of microbial community composition and activity when the depth of soil layer in tea garden is increased. |INVENTION MODE|Detailed Description|[0022] The technical solutions of the present invention will be clearly and completely described in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0023] All experiments were repeated 3 times except for the specific description, the results were expressed as average values, and P <0.05 indicated significant differences.|[0024] Experiments of the embodiment and the comparative example are collected in a tea garden at five layers of depths (0-20, 20-40, 40-60, 60-80 and 80-100 cm) in a plum home dock village (30 degrees 10 'in north latitude and 120 degrees 5' in east longitude) in western lake region of Hangzhou city in China. The altitude of the research area is 153 meters, and the method belongs to a humid subtropical climate influenced by the monsoon, the annual average temperature is 17.0 ℃ and the annual precipitation is 1533 millimeters. The test soil is loam clay which is developed from Anshan and is formed by no quartz porphyry. The longjing tea is planted in a tea garden with century cultivation history, and the annual yield of the longjing tea is 175 kg/hectare. The organic carbon (SOC) content of the soil tends to decrease with the increase of the soil layer, and the content in the soil layers of 0-20 cm, 20-40 cm, 40-60 cm, 60-80 cm and 80-100 cm is 3.69%, 1.22%, 0.86%, 0.31% and 0.31% respectively.|[0025] Embodiment 1 is a tea garden soil organic carbon lifting method based on deep ploughing and pruning and returning to the field, comprising the following steps:| S1, soil depth layering and deep turning treatment |Layering tea garden soil according to 0-20 cm, 20-40 cm, 40-60 cm, 60-80 cm and 80-100 cm, and adopting mechanical deep turning technology to disturb soil to 80-100 cm depth, so as to break original soil structure but not destroy tea tree root system. After deep turning, the soil is subjected to regional management according to 0-40 cm (surface layer) and 40-100 cm (deep layer) so as to adapt to the carbon cycle characteristics of the soil with different depths;| s2, pruning and directional deep burying |After picking tea in spring, pruning tea trees, and crushing the prunes (branches and leaves) into fragments of 2-5 cm so as to improve the decomposition efficiency;| S3, zonal fertilization |Applying conventional nitrogen-phosphorus-potassium fertilizer (460 kg N/ha, NPK=3:1:1) to surface soil (0-40 cm) to maintain nutrients required by tea plant growth, mixing the deep soil (40-100 cm) with trim pieces (3000 kg/ha) and organic fertilizer (rapeseed cake) (6000 kg/ha), supplementing easily-decomposed carbon components (such as POC and WSOC), activating deep microbial activity, improving the abundance of functional microorganisms (Alphaproteobacteria, sordariomycetes) in the deep soil by deeply burying the trim and the organic fertilizer, promoting the expression of GH48 and cbhI genes, enhancing the activity of carbon degrading enzymes (beta-glucosidase and cellobiohydrolase) (figure 3),|S4, microbial community and moisture regulation|The micro-sprinkling irrigation technology is adopted to maintain the water content of the soil at 60% WHC (water holding capacity) and ensure the water condition required by the metabolic activity of microorganisms.|[0026] Test example 1 Effect of trim particle size on tea garden soil organic carbon lifting Effect|The trimmings were crushed to 0-1 cm, 1-2 cm, 2-3 cm, 4-5 cm, 6-8cm, >10 cm, and six treatment groups were set up, G1:0-1 cm, G2:1-2 cm, G3:2-3 cm, G4;4-5 cm, G5:6-8cm, G6: >10 cm, the remainder of the procedure being as in example 1. The effect of different crushed particle sizes on the mineralization amount of soil after 45 days of microbial community and moisture regulation is shown in table 1.|[0027] TABLE 1|[0028] Note that the different letters after the same column of data represent a significant difference between treatments at P <0.05 level.|[0029] The results show that the particle size of the pruning matters is a key factor influencing the deep carbon fixation effect. When the particle diameter is too small (0-2 cm), the carbon fixation effect is remarkably deteriorated, which is represented by that the mineralization amount of SOC of the G1 and G2 groups is remarkably higher than that of the optimal group, and the mineralization amount of G1 (0-1 cm) is higher than that of G2 (1-2 cm). This phenomenon is attributed to the fact that too small particle size causes a sharp increase in specific surface area, and induces too rapid mineralization in deep soil, which in turn causes the carbon source to be rapidly consumed and thus cannot achieve long-term sequestration. On the contrary, when the particle size is too large (> 5 cm), the carbon fixation effect of the groups G5 and G6 is also poor, and due to the insufficient contact area with soil, the decomposition is slow, and it is difficult to effectively start the microbial carbon fixation process. In the optimal range of 2-5 cm (G3 and G4 groups), the mineralization amount of the SOC is always stable at the lowest level without obvious difference among the groups, so that the optimal balance of the decomposition rate and the microorganism utilization efficiency is realized, and the long-term and stability of deep soil carbon fixation are ensured.|[0030] Test example 2 organic carbon mineralization of different soil layers|1. Test method|1. Example 1 the culture experiments were divided into five treatments according to soil depth (1) 0-20 cm, (2) 20-40 cm, (3) 40-60 cm, (4) 60-80 cm and (5) 80-100 cm, each treatment being repeated three times. After air drying, 400 g fresh soil was calibrated to 60% of its Water Holding Capacity (WHC). Each soil sample was divided into two parts, 200 g soil for CO2 quantification and 200 g for destructive sampling protocols. The soil was placed in a 500 mL glass vessel with a mass density of 1.3 g cm 3.|[0031] 2. The release amount of CO 2 was measured by alkali absorption-titration, the culture vessel and an absorption vessel containing 10 mL of 0.2 mol/L NaOH solution were placed in a 500 mL closed bottle, and the soil sample was cultured at a constant temperature of 25℃for 45 days. To maintain a constant humidity environment of 60% field Water Holding Capacity (WHC), water was replenished by weighing after each CO 2 measurement.|[0032] 3. Three blank control bottles (treatment method identical to test group) were set for the test to correct the bottle headspace CO 2 background value. After the NaOH absorption solution was changed, CO 2 was quantitatively measured on days 1, 3, 5, 10, 15, 30 and 45, respectively.|[0033] 2. Description of results|As can be seen from fig. 3, in the tea garden ecosystem, the organic carbon mineralization rate showed a significant decrease trend (P < 0.05) with increasing soil layer depth. The cumulative release amount of CO 2 in each soil layer (0-20 cm, 20-40 cm, 40-60 cm, 60-80 cm and 80-100 cm) is 842, 615, 550, 459 and 431 mg/kg respectively. Statistical analysis shows that the release amount of CO 2 in different soil layers is obviously different (P < 0.05), and the release amount is 80-100 cm =60-80 cm <40-60 cm <20-40 cm <0-20 cm.|[0034] Test example 3 Effect of different fertilization modes on mineralization amount of soil|1. Test method (traditional treatment)|The difference from example 1 is that:| 0-40 cm layers of urea (300 kg/ha) and phosphorus-potassium compound fertilizer (100 kg/ha); | 40-100 cm layers, mixing 3000 kg/ha of prune fragments and 6000 kg/ha of organic fertilizer (rapeseed cakes). |[0035] 2. Description of results|TABLE 2|[0036] Note that the MBC content of the deep soil is increased by 25% and the beta-glucosidase activity is increased by 40%.|[0037] Test example 4 Effect of soil layer depth on tea garden soil cumulative CO 2 emission dynamics|1. Test method|After the air drying treatment, 400 g of fresh soil in example 1 was taken and its humidity was adjusted to 60% of maximum Water Holding Capacity (WHC). Each soil sample was divided into two parts, 200 g for CO 2 quantitative analysis and 200 g for destructive sampling. Soil was filled into 500 mL glass containers at a volume weight of 1.3 g cm -3.|[0038] The amount of released CO 2 was determined by means of an alkaline absorption-titration method. The specific steps are that a container filled with soil and a small beaker filled with 10mL of 0.2 mol.L -1 NaOH solution are placed in a 500 mL sealed bottle together, and are cultured for 45 days at 25 ℃. After each CO 2 measurement, water was added gravimetrically to maintain the soil moisture at 60% WHC. Three additional blank containers (without soil) were set as controls to correct the background value of CO 2 in the headspace of the sealed bottle.|[0039] 2. Analysis of results|In the tea garden ecosystem, the organic carbon mineralization rate showed a significant trend of decrease (P < 0.05) with increasing soil layer depth (fig. 3 a). The total CO 2 release amounts for the soil layers 0-20 cm, 20-40 cm, 40-60 cm, 60-80 cm, and 80-100 cm were 842, 615, 550, 459, and 431 mg kg -1, respectively (fig. 3 b). Furthermore, each soil layer accumulated CO 2 release exhibited a significant level difference (P < 0.05) expressed as 80-100 cm = 60-80 cm <40-60 cm <20-40 cm <0-20 cm (fig. 3 b).|[0040] Test example 5 Effect of soil layer depth on cbhI Gene and GH48 Gene abundance in tea garden soil|1. Test method|Three samples of 0.2 g soil from example 1 were subjected to DNA extraction using FAST DNA SPIN extraction kit and further purified via OMEGA purification kit. The concentration and quality of the extracted DNA are detected by using a Nanodrop ND-1000 spectrophotometer, and the purified DNA sample is stored in an ultralow temperature environment of-70 ℃ until the subsequent molecular analysis.|[0041] Fungal Internal Transcribed Spacer (ITS) sequence amplification uses an ITS3F/ITS4R primer combination and bacterial 16S ribosomal RNA (rRNA) gene region amplification uses a 515F/806R primer system. The PCR reaction was performed on an ABI GeneAmp cube 9700 type PCR apparatus, with a reaction system of 20. Mu.L containing TransStartFastpfu DNA polymerase. The thermal cycling procedure was 95℃pre-denaturation for 180 seconds, followed by 35 (ITS) or 27 (16S rRNA) cycles, each cycle consisting of 95℃denaturation for 30 seconds, 55℃annealing for 30 seconds and 72℃extension for 45 seconds, and finally 72℃final extension for 600 seconds.|[0042] The amplified products are purified to construct a sequencing library, a TruSeqTM DNA library construction method is adopted to prepare a high-throughput sequencing library, double-end sequencing is carried out on a Nextseq 2000 platform, and the original data are stored in a FASTQ format and are subjected to sequence quality control. Bioinformatics analysis was based on the QIIME2 platform, using DADA2 algorithm (CALLAHAN ET al., 2016) for sequence quality control and feature table construction. Sequences were clustered into Amplicon Sequence Variants (ASVs) and taxonomic annotation was done using the Silva 138 database.|[0043] 2. Analysis of results|At 15 and 45 days of culture, cbhI and GH48 gene abundances were significantly reduced in each soil layer below 0-20 cm (fig. 4 a-d). Specifically, on day 15, the abundance of cbhI gene was significantly lower in the 80-100 cm soil layers than in the 20-40 cm, 40-60 cm, and 60-80 cm soil layers, with no significant difference observed between the three intermediate soil layers (fig. 4 a). For GH48 gene, the abundance distribution rule on day 15 is 20-40 cm >40-60 cm >60-80 cm =80-100 cm. By day 45, the law was slightly adjusted to 20-40 cm = 40-60 cm >60-80 cm >80-100 cm (fig. 4 c-d).|[0044] Test example 6 Effect of soil layer depth on enzyme Activity in tea garden soil|1. Test method|The cellobiohydrolase (Cellobiohydrolase) is determined by a3, 5 dinitrosalicylic acid colorimetric method, and the cellobiohydrolase activity is determined by using sodium carboxymethyl cellulose as a substrate. A brief procedure was followed by weighing 0.5 g fresh soil, mixing with 4. 4 mL sodium acetate buffer 50 mM (pH 5.0) containing 1% sodium carboxymethylcellulose, and culturing at 37℃for 24 hours. After the reaction was completed, the test tube was placed in a boiling water bath for 10 minutes to terminate the reaction. After centrifugation, the supernatant was taken and the resulting reducing sugar content was determined by 3, 5-dinitrosalicylic acid (DNS) colorimetry at a wavelength of 540 nm.|[0045] Beta-glucosidase (beta-glucosidase) was colorimetrically performed using nitrophenol. 1.0 g fresh soil samples were weighed and mixed with 4 mL of 25 mM modified universal buffer (MUB, pH 6.0) and 1 mL of 25 mM p-nitrophenyl-beta-D-glucopyranoside (pNPG) substrate solution and incubated at 37℃for 1 hour. Immediately after the reaction was completed, the sample was cooled on ice, and 4 mL of 0.1M Tris-HCl buffer (pH 12.0) and 1 mL of 0.5M CaCl 2 solution were added to terminate the reaction and develop color. After centrifugation, the release of p-nitrophenol (pNP) in the supernatant was determined using a spectrophotometer at 405 nm wavelength.|[0046] 2. Analysis of results|The beta-glucosidase activities of subsurface layers (20-40, 40-60, 60-80, 80-100 cm) were significantly reduced (P < 0.05) by 12%, 58%, 63% and 69%, respectively, on day 15 compared to the superficial layer soil (0-20 cm). Except for no significant differences between the depths of 40-60 cm and 60-80 cm, there were statistical differences between treatments (fig. 5 a). By day 45, the β -glucosidase activities of these same soil layers were significantly reduced (P < 0.05) by 50%, 66%, 75% and 75%, respectively, compared to the superficial soil. Except that there was no significant difference between the two deepest soil layers, there was a significant difference between the remaining treatments (fig. 5 b).|[0047] On day 15, cellobiohydrolase activity showed a significant difference between depths (P < 0.05), except for 20-40 cm and 60-80 cm soil layers, and a decreasing trend with increasing depth (fig. 5 c). By day 45, the surface cellobiohydrolase activity was still significantly higher (P < 0.05) than all deep soil, with no significant difference between depths 20-100 cm (fig. 5 d).|[0048] Test example 7 influence of soil layer depth on tea garden soil carbon reservoir content|1. Test method|(1) Water-soluble organic carbon (WSOC):| The water-soluble organic carbon (WSOC) was measured using a deionized water leaching method. Accurately weighing a certain amount of fresh soil, adding deionized water according to a certain water-soil ratio (such as 1:5), oscillating at constant temperature, centrifuging, filtering supernatant with a 0.45 μm microporous filter membrane, and measuring the concentration of organic carbon in the filtrate by using a total organic carbon analyzer (TOC analyzer). |[0049] (2) Microbial Biomass Carbon (MBC):| The Microbial Biomass Carbon (MBC) adopts a chloroform fumigation-potassium sulfate leaching method. Equal amounts of fresh soil were split into two parts, one part was fumigated with ethanol-free chloroform in the dark at 25 ℃ for 24 hours and the other part served as a non-fumigated control. After fumigation, both were leached with 0.5M K 2SO4 solution and the organic carbon content of the leaching solution was determined. |[0050] (3) Particulate Organic Carbon (POC):| Particulate Organic Carbon (POC) was determined by physical grouping separation. After dispersing the air-dried soil with a sodium hexametaphosphate solution, wet sieving the air-dried soil by a 53 mu m sieve, and obtaining the organic particles with the particle diameter of more than 53 mu m which are reserved on the sieve as the POC component. After collecting, drying, weighing the component, the carbon content thereof was measured using an elemental analyzer. |[0051] (4) Mineral bound organic carbon (MAOC):| The determination of mineral bound organic carbon (MAOC) is based on the remainder after POC separation. The soil suspension passing through the 53 μm mesh after wet sieving (i.e., the portion after POC removal) contained MAOC, which was collected, dried, and ground, and then its carbon content was measured by an elemental analyzer. |[0052] 2. Analysis of results|Regardless of the length of cultivation time, the soil Particle Organic Carbon (POC) content of the 0-20 cm soil layers is always significantly higher than (P < 0.05) deeper soil layers, and the POC content of the 20-40 cm soil layers is significantly higher than (P < 0.05) 40-60 cm, 60-80 cm and 80-100 cm soil layers. No significant differences were found between the soil layers 40-60 cm, 60-80 cm and 80-100 cm (fig. 6a and 6 b).|[0053] On day 15 of culture, the soil mineral bound organic carbon (MAOC) content follows the following sequence (P < 0.05) 0-20 cm >20-40 cm >40-60 cm >60-80 cm = 80-100 cm (FIG. 6 c). By day 45, the order becomes (P < 0.05): 0-20 cm >20-40 cm =40-60 cm =60-80 cm =80-100 cm (fig. 6 d).|[0054] Similarly, on day 15 of culture, the water-soluble organic carbon (WSOC) content of each soil layer was in the order of (P < 0.05): 0-20 cm >20-40 cm >40-60 cm >60-80 cm =80-100 cm (FIG. 6 e). But by day 45, the order became (P < 0.05) 0-20 cm >20-40 cm >40-60 cm >60-80 cm >80-100 cm (FIG. 6 f);| On day 15 of the culture, the content of carbon (MBC) in the soil microorganism biomass is (P < 0.05): 0-20 cm >20-40 cm >40-60 cm >60-80 cm >80-100 cm (FIG. 6 g). This trend remained consistent on day 45, but no significant difference was exhibited in MBC content between 60-80 cm and 80-100 cm soil layers (fig. 6 h). |[0055] Test example 8 composition of bacterial and fungal communities in tea garden soil at different soil layer depths|1. Test method|The water is regulated and controlled for 15 days and 45 days, and the water is sampled once respectively, and the water is expressed by adopting a heat map form, so that the tea garden soil bacteria (a, b) and fungi (c, d) community composition is expressed under different soil layer depths. Group designations with a relative abundance of greater than 1% are shown (as in fig. 4).|[0056] 2. Analysis of results|At both time points, the relative abundance of α -amoxycillium (Alphaproteobacteria) and bacillus (bacili) in the bacteria decreased significantly with increasing soil layers, but there was no significant difference between the three deepest soil layers. In contrast, the relative abundance of the class of armored cocci (Ktedonobacteria) and AD3 increased with increasing depth (fig. 7a, b).|[0057] The relative abundance of the fecal crustaceans (Sordariomycetes) and tremella bacteria (Tremellomycetes) in fungi is significantly reduced as the soil layer deepens. In contrast, the abundance of mortierella (Mortierellomycetes) and ascomycetes (Dothideomycetes) increased significantly with depth gradient at day 15, and this trend continued until day 45 (fig. 7c, d).|[0058] The depth of the tea garden soil layer is increased, and the mineralization of organic carbon in the soil is inhibited by the synergistic change of the microbial community composition and the activity. As the depth of tea garden soil increases, SOC breakdown rate, particulate Organic Carbon (POC) content, water Soluble Organic Carbon (WSOC) levels, microbial Biomass Carbon (MBC), β -glucosidase and cellobiohydrolase activity, and GH48 and cbhI gene marker concentrations decrease significantly. These decreasing trends of readily available carbon components, extracellular enzyme activities and functional gene markers are the main driving factors that lead to the decrease in the SOC breakdown process with depth. In addition, the increase in soil depth significantly alters the microbial community structure and cluster distribution, particularly affecting the relative abundance of key taxa (including Alphaproteobacteria, bacelli, sordariomycetes, tremellomycetes, mortierellomycetes, and Dothideomycetes), and thus affecting the rate of SOC breakdown (see fig. 8).|[0059] This study demonstrates that increasing soil depth significantly alters the soil microbial community characteristics by reducing the carbon degradation functional gene markers and enzyme activity, thereby reducing the rate of SOC decomposition and weakening the soil carbon release process. The research results show that in tea garden management, the adoption of deep-ploughing cultivation assisted with the fertilization system of pruning residues and returning to the field has urgent need for improving the SOC storage capacity.|[0060] Comparative example 1|The difference from example 1 is that the deep-ploughing depth is 70 cm, the surface soil is 0-20 cm, and the deep soil is 20-70 cm.|[0061] The results show that the physical channel for downward transport of the carbon source is blocked due to insufficient deep-drawing depth. It is directly expressed that the SOC mineralization amount of 80-100 cm soil layers is increased to 338 mg/kg, and the carbon fixation efficiency is reduced by 11.9% compared with that of the embodiment 1 (302 mg/kg). The result shows that the deep-turning depth reaching 80-100 cm and the division modes of the surface layer and the deep soil are necessary means for realizing the expected carbon fixing effect.|[0062] Comparative example 2|The difference from example 1 is that only 6000 kg/ha of organic fertilizer was applied in the deep soil without the addition of clippings.|[0063] The results indicate that, although organic fertilizers provide a stable carbon source, the deep microbial community cannot be activated rapidly due to the lack of readily decomposable carbon components contained in the prune fragments. The method is directly characterized in that the mineralization amount of SOC is increased to 360 mg/kg, the carbon fixation efficiency is reduced by about 19.2% compared with that of the embodiment 1, and meanwhile, the initial colonization and the abundance increase of key carbon circulation functional flora such as Alphaproteobacteria are also obviously delayed. Therefore, the synergistic effect generated by the mixed application of the pruning and the organic fertilizer in deep soil is a key for realizing quick start and maintaining long-term high-efficiency carbon fixation.|[0064] The above examples illustrate only a few embodiments of the invention, which are described in detail and are not to be construed as limiting the scope of the invention. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the invention, which are all within the scope of the invention. Accordingly, the scope of protection of the present invention is to be determined by the appended claims. (CN121176213)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of soil remediation, in particular to a tea garden soil organic carbon lifting method based on deep ploughing and pruning returning.|BACKGROUND ART|[0002] Tea leaves are one of three major world beverages, and main chemical components such as catechin, caffeine and the like have a plurality of benefits on human health. In modern tea garden management, scientific planting and management are core factors for guaranteeing excellent quality and stable yield of tea. However, the current tea garden soil organic carbon lifting technology mainly has three technical bottlenecks.|[0003] First is the problem of carbon cycle imbalance. The existing management measures are concentrated on surface soil (0-20 cm), and the organic carbon content of the soil can be improved in a short period of time when the pruning is returned to the field, but the decomposition rate of the organic carbon is too high due to high activity of microorganisms and enzymes in the surface soil, so that long-term solid storage is difficult to realize. In contrast, deep soil (below 40 cm) has the natural advantage of low mineralization rate, but the carbon fixation potential is not effectively developed and utilized for a long time due to insufficient carbon input. And secondly, the defect of microorganism regulation and control. The existing cultivation mode has obvious limitation on the regulation and control of soil microbial communities, particularly the cognitive insufficiency of functional microbial communities on deep soil, the effective regulation and control of soil organic carbon mineralization inhibition bacterial communities are difficult, and an effective soil organic carbon protection mechanism cannot be established. Third is a lack of technical synergy. In the traditional management, all technical links are mutually split, deep-ploughing cultivation is asynchronous with organic carbon supplementation, fertilization strategies are not matched with microbial regulation, a synergistic action chain of carbon input, community regulation and mineralization inhibition cannot be formed, and the continuous accumulation of organic carbon reserves in soil is severely restricted.|[0004] Although studies have revealed that tea tree pruning returns to the field to improve soil fertility and carbon storage, the prior art is still limited to traditional surface layer applications and fails to achieve directional migration of carbon sources into deep soil. Meanwhile, although the conventional cultivation depth (less than or equal to 60 cm) and the fertilization scheme provide 'deep fertilization of base fertilizer', the aim is only to improve the fertilizer utilization rate, and the vertical distinction characteristic of the soil carbon cycle of 'surface hypersalinity and deep hypoalinity' cannot be recognized and utilized, so that the targeted carbon management of the tea garden soil cannot be realized.|DISCLOSURE|Disclosure of Invention|[0005] In order to solve the problems, the invention provides a tea garden soil organic carbon lifting method based on deep turning and pruning to return to the field. According to the invention, through the combination of deep turning and pruning returning, the carbon fixing capability of the tea garden soil is obviously improved, and the residence time of carbon in the soil is prolonged and the overall carbon fixing efficiency is improved by reducing the mineralization rate of deep SOC. Meanwhile, the microbial community structure is optimized, and the gene abundance is increased. And the utilization rate of resources is improved by returning the pruning to the field.|[0006] The invention provides a tea garden soil organic carbon lifting method based on deep ploughing and pruning returning, which specifically comprises the following steps:| s1, layering tea garden soil, deeply turning the soil to 80-100 cm, breaking the original soil structure, but not damaging the root system of tea trees, and dividing the soil layer into a soil surface layer and a soil deep layer; | S2, pruning tea trees after picking tea, and crushing the prunes to 2-5 cm to obtain prune fragments; | s3, applying a compound fertilizer to the surface layer of the soil, and applying the pruning fragments and the organic fertilizer in the S2 to the deep layer of the soil; | s4, carrying out moisture management on the soil through micro-spray irrigation, regulating microbial communities, and improving organic carbon in the soil of the tea garden. |[0007] Preferably, the depth of the soil surface layer in the step S1 is 0-40 cm, and the depth of the soil deep layer is 40-100 cm.|[0008] Preferably, the compound fertilizer in the step S2 is a nitrogen-phosphorus-potassium fertilizer, wherein the N: P: K=3:1:1 of the nitrogen-phosphorus-potassium fertilizer, the nitrogen application amount of the compound fertilizer is 450-480 kg N/ha, the application amount of the pruning is 2800-3200-kg/ha, the application amount of the organic fertilizer is 5700-6300 kg/ha, the organic fertilizer is a rapeseed cake or a mixture of a rapeseed cake and a farmyard manure, the rapeseed cake accounts for more than or equal to 80 wt%, and the C/N ratio is (20-25): 1.|[0009] Preferably, the water content of the soil after micro-sprinkling irrigation in the step S4 is 55% -65%, the water management time is more than or equal to 7 days, and the microbial community regulation comprises the steps of promoting Alphaproteobacteria, sordariomycetes microbial communities and inhibiting Mortierellomycetes, dothideomycetes microbial communities.|[0010] The deep soil is deeply ploughed to 80-100 cm, which is a core technological breakthrough for realizing efficient carbon fixation of tea garden soil, the necessity of the deep soil is derived from the vertical diversity characteristic of organic carbon mineralization of the tea garden soil, the accumulated and released amount of CO 2 of the tea garden soil is obviously reduced along with the depth, the natural low mineralization advantage of the deep soil provides a theoretical basis for long-term carbon fixation, but the premise is that the original compact soil structure is broken through the deep ploughing technology, and an effective physical channel is constructed for migration of a carbon source to the deep layer.|[0011] The traditional tea garden management has obvious technical bottlenecks, which are mainly represented by insufficient cultivation depth and unbalanced carbon circulation. The existing management measures are concentrated on the soil with the surface layer of 0-20 cm, and the pruned soil is quickly decomposed due to the high mineralization rate of the surface layer after returning to the field, so that long-term carbon fixation is difficult to realize. Conventional cultivation depths generally do not exceed 60 cm, and although the concept of deep application of base fertilizer is proposed, the goal is limited to improving fertilizer utilization rate, and the key characteristic of low mineralization of deep soil cannot be recognized and utilized. More importantly, deep soil is in a "carbon starvation" state for a long period of time, and the carbon fixation potential of the deep soil is not effectively exploited. The invention breaks through the depth limit of traditional cultivation by lifting the deep turning depth to 80-100 cm, and establishes a vertical partition management system of 'surface layer yield maintenance and deep carbon fixation' for the first time.|[0012] The depth of less than 70 cm cannot reach the lowest mineralization zone, and the physical channel for downward delivery of the carbon source is blocked, so that the deep soil is still in a state of insufficient carbon input. Meanwhile, the effective root systems of the tea trees are mainly distributed in the range of 0-60 cm, and 80-100 cm are deeply turned below the root systems, so that the soil structure can be broken, the root systems of the tea trees cannot be damaged, and the balance of technical feasibility and ecological safety is realized.|[0013] Deep turning to 80-100 cm creates a necessary condition for the migration of the pruned fragments and organic fertilizer to the deep layer, thereby triggering a series of synergistic carbon fixation mechanisms. Deep ploughing not only delivers a carbon source, but also successfully activates the deep functional microflora. After the deep ploughing and returning the complex pruning material to the field, the activity of beta-glucosidase in deep soil is reduced, the gene abundance of GH48 is reduced, and the activity of cellobiohydrolase is obviously weakened. This mode of microbial control, which "activates but inhibits hypersalinity", is the central mechanism by which deep-turning technology interacts with the trimmings track and field association.|[0014] From the aspect of microbial community structure, the directional regulation and control of key flora is realized by deep turning to 80-100 cm. Although the relative abundance of high mineralization flora such as Mortierellomycetes and Dothideomycetes in deep soil increases with depth, the enrichment of low mineralization functional flora such as Alphaproteobacteria and Sordariomycetes is promoted due to deep ploughing and returning of the pruning object to the field, and simultaneously the activity of carbon degrading enzyme and the expression of functional genes are inhibited, so that the overall mineralization rate is still obviously reduced. The reconstruction of the community structure changes the micro-ecological environment of deep soil by 80-100 cm deep turning, creates favorable conditions for carbon source input, and guides the succession of microbial communities to the direction favorable for carbon fixation.|[0015] In addition, 80-100 cm deep turning is a precondition for realizing layered and accurate management of tea gardens. The compound fertilizer is applied on the surface layer 0-40 cm to maintain the nutrients required by the growth of tea trees and ensure the annual yield of spring tea, and the pruning and organic fertilizer are mixed in the deep layer 40-100 cm to concentrate on long-term carbon fixation. The strategy of upper layer production-protecting and lower layer carbon fixation unifies the production targets and ecological targets which are mutually independent in the past into a set of complete technical scheme. If the deep turning depth is insufficient, the deep soil is still in a state of lack of carbon input, vertical partition management cannot be realized, surface layer trimmings can be mineralized continuously and rapidly, and the deep carbon fixation potential cannot be exerted.|[0016] According to the invention, the carbon fixation efficiency of deep soil is maximized by crushing the pruning to 2-5 cm, the mineralization amount of SOC is improved due to the fact that the specific surface area is too small (2 cm), the deep hypersalinity flora (Mortierellomycetes, dothideomycetes) is triggered to be excessively activated, the activity of beta-glucosidase is obviously improved, a carbon source is rapidly mineralized and released, the mineralization amount of SOC is improved due to slow decomposition and poor contact of soil when the particle size is too large (5 cm), the decomposition carbon component is not provided for deep functional microorganisms (Alphaproteobacteria, sordariomycetes) in time, GH48 and cbhI gene expression is delayed, and the optimal window period for microbial community regulation is missed.|[0017] Compared with the prior art, the invention has the beneficial technical effects that:| Firstly, the deep turning depth is set to 80-100 cm, an effective channel is constructed for the migration of a carbon source to a deep layer, and a zonal fertilization strategy based on the vertical difference of carbon circulation is combined, chemical fertilizers are applied to the surface layer of 0-40 cm to ensure the growth and yield of tea trees, and pruning matters and organic fertilizers are applied in the deep layer of 40-100 cm to successfully activate the functions of deep microorganisms, so that the mineralization rate of organic carbon in the deep layer soil is reduced by 30-49%, and the detention time of carbon in the soil is remarkably prolonged. |[0018] Secondly, the invention optimizes the microbial community structure, promotes the enrichment of Alphaproteobacteria, sordariomycetes and other beneficial bacteria by directional regulation, simultaneously inhibits Mortierellomycetes, dothideomycetes and other hypersalinity bacteria, reduces the beta-glucosidase activity of deep soil by 40% -75%, reduces the GH48 gene abundance by about 20%, and effectively weakens the carbon metabolism function of microorganisms, thereby enhancing the organic carbon fixation capability of soil. In addition, the invention realizes the optimal balance of the decomposition rate and the microorganism utilization efficiency by precisely controlling the particle size of the pruning material (2-5 cm), and avoids the problems of rapid mineralization caused by too small particle size and slow decomposition caused by too large particle size.|[0019] In the aspect of resource utilization, the utilization rate of returning the pruning objects to the field reaches 95%, the input of external organic fertilizer is reduced by about 20%, and the efficient recycling of tea garden waste is realized. More importantly, the invention realizes layered accurate management, adopts a differentiated fertilization strategy aiming at the carbon circulation characteristics of soil with different depths, unifies two previous mutually independent targets of 'upper layer yield-keeping' and 'lower layer carbon fixation' into a complete technical scheme for the first time, maximizes the carbon fixation effect while guaranteeing the tea yield, and realizes the collaborative improvement of the economic benefit and the ecological benefit of the tea garden.|DRAWINGS DESCRIPTION|[0020] The invention is further described with reference to the following description of the drawings.|[0021] FIG. 1 is a process flow diagram of the present invention compared with a conventional method;| fig. 2 is a flow chart of a tea garden deep soil carbon fixation lifting technology in embodiment 1 of the invention; | FIG. 3 is a graph showing the effect of soil layer depth on the accumulated CO 2 emission dynamics of tea garden soil in test example 2 according to the present invention, wherein FIG. 3a is a graph showing the accumulated CO 2 release curves of different soil layer depths, and FIG. 3b is a histogram showing the total CO 2 release amount of each soil layer after 45 days of cultivation; | FIG. 4 is a graph showing the effect of soil layer depth on the abundance of cbhI gene and GH48 gene in tea garden soil in test example 5 of the invention, wherein FIGS. 4a and 4b are the abundance of cbhI gene on day 15 and 45 of culture, respectively, and FIGS. 4c and 4d are the abundance of GH48 gene on day 15 and 45 of culture, respectively; | FIG. 5 is a graph showing the effect of soil layer depth on enzyme activity in tea garden soil in test example 6 of the present invention, wherein FIG. 5a and FIG. 5b are the beta-glucosidase activity on day 15 and day 45 of cultivation, respectively, and FIG. 5c and FIG. 5d are the cellobiohydrolase activity on day 15 and day 45 of cultivation, respectively; | FIG. 6 is a graph showing the effect of soil layer depth on the carbon content of tea garden soil in test example 7 according to the present invention, wherein FIG. 6a and FIG. 6b are POC content on 15 th and 45 th of cultivation, FIG. 6c and FIG. 6d are MAOC content on 15 th and 45 th of cultivation, FIG. 6e and FIG. 6f are WSOC content on 15 th and 45 th of cultivation, respectively, and FIG. 6g and FIG. 6h are MBC content on 15 th and 45 th of cultivation, respectively; | FIG. 7 is a graph showing the composition of bacterial and fungal colonies in tea garden soil at different soil layer depths in test example 8 according to the present invention, wherein FIGS. 7a and 7b are thermal graphs showing the composition of bacterial colonies on 15 th and 45 th of cultivation, respectively, and FIGS. 7c and 7d are thermal graphs showing the composition of fungal colonies on 15 th and 45 th of cultivation, respectively; | FIG. 8 is a schematic diagram showing the mechanism of inhibiting mineralization of organic carbon in soil by synergistic change of microbial community composition and activity when the depth of soil layer in tea garden is increased. |INVENTION MODE|Detailed Description|[0022] The technical solutions of the present invention will be clearly and completely described in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0023] All experiments were repeated 3 times except for the specific description, the results were expressed as average values, and P <0.05 indicated significant differences.|[0024] Experiments of the embodiment and the comparative example are collected in a tea garden at five layers of depths (0-20, 20-40, 40-60, 60-80 and 80-100 cm) in a plum home dock village (30 degrees 10 'in north latitude and 120 degrees 5' in east longitude) in western lake region of Hangzhou city in China. The altitude of the research area is 153 meters, and the method belongs to a humid subtropical climate influenced by the monsoon, the annual average temperature is 17.0 ℃ and the annual precipitation is 1533 millimeters. The test soil is loam clay which is developed from Anshan and is formed by no quartz porphyry. The longjing tea is planted in a tea garden with century cultivation history, and the annual yield of the longjing tea is 175 kg/hectare. The organic carbon (SOC) content of the soil tends to decrease with the increase of the soil layer, and the content in the soil layers of 0-20 cm, 20-40 cm, 40-60 cm, 60-80 cm and 80-100 cm is 3.69%, 1.22%, 0.86%, 0.31% and 0.31% respectively.|[0025] Embodiment 1 is a tea garden soil organic carbon lifting method based on deep ploughing and pruning and returning to the field, comprising the following steps:| S1, soil depth layering and deep turning treatment |Layering tea garden soil according to 0-20 cm, 20-40 cm, 40-60 cm, 60-80 cm and 80-100 cm, and adopting mechanical deep turning technology to disturb soil to 80-100 cm depth, so as to break original soil structure but not destroy tea tree root system. After deep turning, the soil is subjected to regional management according to 0-40 cm (surface layer) and 40-100 cm (deep layer) so as to adapt to the carbon cycle characteristics of the soil with different depths;| s2, pruning and directional deep burying |After picking tea in spring, pruning tea trees, and crushing the prunes (branches and leaves) into fragments of 2-5 cm so as to improve the decomposition efficiency;| S3, zonal fertilization |Applying conventional nitrogen-phosphorus-potassium fertilizer (460 kg N/ha, NPK=3:1:1) to surface soil (0-40 cm) to maintain nutrients required by tea plant growth, mixing the deep soil (40-100 cm) with trim pieces (3000 kg/ha) and organic fertilizer (rapeseed cake) (6000 kg/ha), supplementing easily-decomposed carbon components (such as POC and WSOC), activating deep microbial activity, improving the abundance of functional microorganisms (Alphaproteobacteria, sordariomycetes) in the deep soil by deeply burying the trim and the organic fertilizer, promoting the expression of GH48 and cbhI genes, enhancing the activity of carbon degrading enzymes (beta-glucosidase and cellobiohydrolase) (figure 3),|S4, microbial community and moisture regulation|The micro-sprinkling irrigation technology is adopted to maintain the water content of the soil at 60% WHC (water holding capacity) and ensure the water condition required by the metabolic activity of microorganisms.|[0026] Test example 1 Effect of trim particle size on tea garden soil organic carbon lifting Effect|The trimmings were crushed to 0-1 cm, 1-2 cm, 2-3 cm, 4-5 cm, 6-8cm, >10 cm, and six treatment groups were set up, G1:0-1 cm, G2:1-2 cm, G3:2-3 cm, G4;4-5 cm, G5:6-8cm, G6: >10 cm, the remainder of the procedure being as in example 1. The effect of different crushed particle sizes on the mineralization amount of soil after 45 days of microbial community and moisture regulation is shown in table 1.|[0027] TABLE 1|[0028] Note that the different letters after the same column of data represent a significant difference between treatments at P <0.05 level.|[0029] The results show that the particle size of the pruning matters is a key factor influencing the deep carbon fixation effect. When the particle diameter is too small (0-2 cm), the carbon fixation effect is remarkably deteriorated, which is represented by that the mineralization amount of SOC of the G1 and G2 groups is remarkably higher than that of the optimal group, and the mineralization amount of G1 (0-1 cm) is higher than that of G2 (1-2 cm). This phenomenon is attributed to the fact that too small particle size causes a sharp increase in specific surface area, and induces too rapid mineralization in deep soil, which in turn causes the carbon source to be rapidly consumed and thus cannot achieve long-term sequestration. On the contrary, when the particle size is too large (> 5 cm), the carbon fixation effect of the groups G5 and G6 is also poor, and due to the insufficient contact area with soil, the decomposition is slow, and it is difficult to effectively start the microbial carbon fixation process. In the optimal range of 2-5 cm (G3 and G4 groups), the mineralization amount of the SOC is always stable at the lowest level without obvious difference among the groups, so that the optimal balance of the decomposition rate and the microorganism utilization efficiency is realized, and the long-term and stability of deep soil carbon fixation are ensured.|[0030] Test example 2 organic carbon mineralization of different soil layers|1. Test method|1. Example 1 the culture experiments were divided into five treatments according to soil depth (1) 0-20 cm, (2) 20-40 cm, (3) 40-60 cm, (4) 60-80 cm and (5) 80-100 cm, each treatment being repeated three times. After air drying, 400 g fresh soil was calibrated to 60% of its Water Holding Capacity (WHC). Each soil sample was divided into two parts, 200 g soil for CO2 quantification and 200 g for destructive sampling protocols. The soil was placed in a 500 mL glass vessel with a mass density of 1.3 g cm 3.|[0031] 2. The release amount of CO 2 was measured by alkali absorption-titration, the culture vessel and an absorption vessel containing 10 mL of 0.2 mol/L NaOH solution were placed in a 500 mL closed bottle, and the soil sample was cultured at a constant temperature of 25℃for 45 days. To maintain a constant humidity environment of 60% field Water Holding Capacity (WHC), water was replenished by weighing after each CO 2 measurement.|[0032] 3. Three blank control bottles (treatment method identical to test group) were set for the test to correct the bottle headspace CO 2 background value. After the NaOH absorption solution was changed, CO 2 was quantitatively measured on days 1, 3, 5, 10, 15, 30 and 45, respectively.|[0033] 2. Description of results|As can be seen from fig. 3, in the tea garden ecosystem, the organic carbon mineralization rate showed a significant decrease trend (P < 0.05) with increasing soil layer depth. The cumulative release amount of CO 2 in each soil layer (0-20 cm, 20-40 cm, 40-60 cm, 60-80 cm and 80-100 cm) is 842, 615, 550, 459 and 431 mg/kg respectively. Statistical analysis shows that the release amount of CO 2 in different soil layers is obviously different (P < 0.05), and the release amount is 80-100 cm =60-80 cm <40-60 cm <20-40 cm <0-20 cm.|[0034] Test example 3 Effect of different fertilization modes on mineralization amount of soil|1. Test method (traditional treatment)|The difference from example 1 is that:| 0-40 cm layers of urea (300 kg/ha) and phosphorus-potassium compound fertilizer (100 kg/ha); | 40-100 cm layers, mixing 3000 kg/ha of prune fragments and 6000 kg/ha of organic fertilizer (rapeseed cakes). |[0035] 2. Description of results|TABLE 2|[0036] Note that the MBC content of the deep soil is increased by 25% and the beta-glucosidase activity is increased by 40%.|[0037] Test example 4 Effect of soil layer depth on tea garden soil cumulative CO 2 emission dynamics|1. Test method|After the air drying treatment, 400 g of fresh soil in example 1 was taken and its humidity was adjusted to 60% of maximum Water Holding Capacity (WHC). Each soil sample was divided into two parts, 200 g for CO 2 quantitative analysis and 200 g for destructive sampling. Soil was filled into 500 mL glass containers at a volume weight of 1.3 g cm -3.|[0038] The amount of released CO 2 was determined by means of an alkaline absorption-titration method. The specific steps are that a container filled with soil and a small beaker filled with 10mL of 0.2 mol.L -1 NaOH solution are placed in a 500 mL sealed bottle together, and are cultured for 45 days at 25 ℃. After each CO 2 measurement, water was added gravimetrically to maintain the soil moisture at 60% WHC. Three additional blank containers (without soil) were set as controls to correct the background value of CO 2 in the headspace of the sealed bottle.|[0039] 2. Analysis of results|In the tea garden ecosystem, the organic carbon mineralization rate showed a significant trend of decrease (P < 0.05) with increasing soil layer depth (fig. 3 a). The total CO 2 release amounts for the soil layers 0-20 cm, 20-40 cm, 40-60 cm, 60-80 cm, and 80-100 cm were 842, 615, 550, 459, and 431 mg kg -1, respectively (fig. 3 b). Furthermore, each soil layer accumulated CO 2 release exhibited a significant level difference (P < 0.05) expressed as 80-100 cm = 60-80 cm <40-60 cm <20-40 cm <0-20 cm (fig. 3 b).|[0040] Test example 5 Effect of soil layer depth on cbhI Gene and GH48 Gene abundance in tea garden soil|1. Test method|Three samples of 0.2 g soil from example 1 were subjected to DNA extraction using FAST DNA SPIN extraction kit and further purified via OMEGA purification kit. The concentration and quality of the extracted DNA are detected by using a Nanodrop ND-1000 spectrophotometer, and the purified DNA sample is stored in an ultralow temperature environment of-70 ℃ until the subsequent molecular analysis.|[0041] Fungal Internal Transcribed Spacer (ITS) sequence amplification uses an ITS3F/ITS4R primer combination and bacterial 16S ribosomal RNA (rRNA) gene region amplification uses a 515F/806R primer system. The PCR reaction was performed on an ABI GeneAmp cube 9700 type PCR apparatus, with a reaction system of 20. Mu.L containing TransStartFastpfu DNA polymerase. The thermal cycling procedure was 95℃pre-denaturation for 180 seconds, followed by 35 (ITS) or 27 (16S rRNA) cycles, each cycle consisting of 95℃denaturation for 30 seconds, 55℃annealing for 30 seconds and 72℃extension for 45 seconds, and finally 72℃final extension for 600 seconds.|[0042] The amplified products are purified to construct a sequencing library, a TruSeqTM DNA library construction method is adopted to prepare a high-throughput sequencing library, double-end sequencing is carried out on a Nextseq 2000 platform, and the original data are stored in a FASTQ format and are subjected to sequence quality control. Bioinformatics analysis was based on the QIIME2 platform, using DADA2 algorithm (CALLAHAN ET al., 2016) for sequence quality control and feature table construction. Sequences were clustered into Amplicon Sequence Variants (ASVs) and taxonomic annotation was done using the Silva 138 database.|[0043] 2. Analysis of results|At 15 and 45 days of culture, cbhI and GH48 gene abundances were significantly reduced in each soil layer below 0-20 cm (fig. 4 a-d). Specifically, on day 15, the abundance of cbhI gene was significantly lower in the 80-100 cm soil layers than in the 20-40 cm, 40-60 cm, and 60-80 cm soil layers, with no significant difference observed between the three intermediate soil layers (fig. 4 a). For GH48 gene, the abundance distribution rule on day 15 is 20-40 cm >40-60 cm >60-80 cm =80-100 cm. By day 45, the law was slightly adjusted to 20-40 cm = 40-60 cm >60-80 cm >80-100 cm (fig. 4 c-d).|[0044] Test example 6 Effect of soil layer depth on enzyme Activity in tea garden soil|1. Test method|The cellobiohydrolase (Cellobiohydrolase) is determined by a3, 5 dinitrosalicylic acid colorimetric method, and the cellobiohydrolase activity is determined by using sodium carboxymethyl cellulose as a substrate. A brief procedure was followed by weighing 0.5 g fresh soil, mixing with 4. 4 mL sodium acetate buffer 50 mM (pH 5.0) containing 1% sodium carboxymethylcellulose, and culturing at 37℃for 24 hours. After the reaction was completed, the test tube was placed in a boiling water bath for 10 minutes to terminate the reaction. After centrifugation, the supernatant was taken and the resulting reducing sugar content was determined by 3, 5-dinitrosalicylic acid (DNS) colorimetry at a wavelength of 540 nm.|[0045] Beta-glucosidase (beta-glucosidase) was colorimetrically performed using nitrophenol. 1.0 g fresh soil samples were weighed and mixed with 4 mL of 25 mM modified universal buffer (MUB, pH 6.0) and 1 mL of 25 mM p-nitrophenyl-beta-D-glucopyranoside (pNPG) substrate solution and incubated at 37℃for 1 hour. Immediately after the reaction was completed, the sample was cooled on ice, and 4 mL of 0.1M Tris-HCl buffer (pH 12.0) and 1 mL of 0.5M CaCl 2 solution were added to terminate the reaction and develop color. After centrifugation, the release of p-nitrophenol (pNP) in the supernatant was determined using a spectrophotometer at 405 nm wavelength.|[0046] 2. Analysis of results|The beta-glucosidase activities of subsurface layers (20-40, 40-60, 60-80, 80-100 cm) were significantly reduced (P < 0.05) by 12%, 58%, 63% and 69%, respectively, on day 15 compared to the superficial layer soil (0-20 cm). Except for no significant differences between the depths of 40-60 cm and 60-80 cm, there were statistical differences between treatments (fig. 5 a). By day 45, the β -glucosidase activities of these same soil layers were significantly reduced (P < 0.05) by 50%, 66%, 75% and 75%, respectively, compared to the superficial soil. Except that there was no significant difference between the two deepest soil layers, there was a significant difference between the remaining treatments (fig. 5 b).|[0047] On day 15, cellobiohydrolase activity showed a significant difference between depths (P < 0.05), except for 20-40 cm and 60-80 cm soil layers, and a decreasing trend with increasing depth (fig. 5 c). By day 45, the surface cellobiohydrolase activity was still significantly higher (P < 0.05) than all deep soil, with no significant difference between depths 20-100 cm (fig. 5 d).|[0048] Test example 7 influence of soil layer depth on tea garden soil carbon reservoir content|1. Test method|(1) Water-soluble organic carbon (WSOC):| The water-soluble organic carbon (WSOC) was measured using a deionized water leaching method. Accurately weighing a certain amount of fresh soil, adding deionized water according to a certain water-soil ratio (such as 1:5), oscillating at constant temperature, centrifuging, filtering supernatant with a 0.45 μm microporous filter membrane, and measuring the concentration of organic carbon in the filtrate by using a total organic carbon analyzer (TOC analyzer). |[0049] (2) Microbial Biomass Carbon (MBC):| The Microbial Biomass Carbon (MBC) adopts a chloroform fumigation-potassium sulfate leaching method. Equal amounts of fresh soil were split into two parts, one part was fumigated with ethanol-free chloroform in the dark at 25 ℃ for 24 hours and the other part served as a non-fumigated control. After fumigation, both were leached with 0.5M K 2SO4 solution and the organic carbon content of the leaching solution was determined. |[0050] (3) Particulate Organic Carbon (POC):| Particulate Organic Carbon (POC) was determined by physical grouping separation. After dispersing the air-dried soil with a sodium hexametaphosphate solution, wet sieving the air-dried soil by a 53 mu m sieve, and obtaining the organic particles with the particle diameter of more than 53 mu m which are reserved on the sieve as the POC component. After collecting, drying, weighing the component, the carbon content thereof was measured using an elemental analyzer. |[0051] (4) Mineral bound organic carbon (MAOC):| The determination of mineral bound organic carbon (MAOC) is based on the remainder after POC separation. The soil suspension passing through the 53 μm mesh after wet sieving (i.e., the portion after POC removal) contained MAOC, which was collected, dried, and ground, and then its carbon content was measured by an elemental analyzer. |[0052] 2. Analysis of results|Regardless of the length of cultivation time, the soil Particle Organic Carbon (POC) content of the 0-20 cm soil layers is always significantly higher than (P < 0.05) deeper soil layers, and the POC content of the 20-40 cm soil layers is significantly higher than (P < 0.05) 40-60 cm, 60-80 cm and 80-100 cm soil layers. No significant differences were found between the soil layers 40-60 cm, 60-80 cm and 80-100 cm (fig. 6a and 6 b).|[0053] On day 15 of culture, the soil mineral bound organic carbon (MAOC) content follows the following sequence (P < 0.05) 0-20 cm >20-40 cm >40-60 cm >60-80 cm = 80-100 cm (FIG. 6 c). By day 45, the order becomes (P < 0.05): 0-20 cm >20-40 cm =40-60 cm =60-80 cm =80-100 cm (fig. 6 d).|[0054] Similarly, on day 15 of culture, the water-soluble organic carbon (WSOC) content of each soil layer was in the order of (P < 0.05): 0-20 cm >20-40 cm >40-60 cm >60-80 cm =80-100 cm (FIG. 6 e). But by day 45, the order became (P < 0.05) 0-20 cm >20-40 cm >40-60 cm >60-80 cm >80-100 cm (FIG. 6 f);| On day 15 of the culture, the content of carbon (MBC) in the soil microorganism biomass is (P < 0.05): 0-20 cm >20-40 cm >40-60 cm >60-80 cm >80-100 cm (FIG. 6 g). This trend remained consistent on day 45, but no significant difference was exhibited in MBC content between 60-80 cm and 80-100 cm soil layers (fig. 6 h). |[0055] Test example 8 composition of bacterial and fungal communities in tea garden soil at different soil layer depths|1. Test method|The water is regulated and controlled for 15 days and 45 days, and the water is sampled once respectively, and the water is expressed by adopting a heat map form, so that the tea garden soil bacteria (a, b) and fungi (c, d) community composition is expressed under different soil layer depths. Group designations with a relative abundance of greater than 1% are shown (as in fig. 4).|[0056] 2. Analysis of results|At both time points, the relative abundance of α -amoxycillium (Alphaproteobacteria) and bacillus (bacili) in the bacteria decreased significantly with increasing soil layers, but there was no significant difference between the three deepest soil layers. In contrast, the relative abundance of the class of armored cocci (Ktedonobacteria) and AD3 increased with increasing depth (fig. 7a, b).|[0057] The relative abundance of the fecal crustaceans (Sordariomycetes) and tremella bacteria (Tremellomycetes) in fungi is significantly reduced as the soil layer deepens. In contrast, the abundance of mortierella (Mortierellomycetes) and ascomycetes (Dothideomycetes) increased significantly with depth gradient at day 15, and this trend continued until day 45 (fig. 7c, d).|[0058] The depth of the tea garden soil layer is increased, and the mineralization of organic carbon in the soil is inhibited by the synergistic change of the microbial community composition and the activity. As the depth of tea garden soil increases, SOC breakdown rate, particulate Organic Carbon (POC) content, water Soluble Organic Carbon (WSOC) levels, microbial Biomass Carbon (MBC), β -glucosidase and cellobiohydrolase activity, and GH48 and cbhI gene marker concentrations decrease significantly. These decreasing trends of readily available carbon components, extracellular enzyme activities and functional gene markers are the main driving factors that lead to the decrease in the SOC breakdown process with depth. In addition, the increase in soil depth significantly alters the microbial community structure and cluster distribution, particularly affecting the relative abundance of key taxa (including Alphaproteobacteria, bacelli, sordariomycetes, tremellomycetes, mortierellomycetes, and Dothideomycetes), and thus affecting the rate of SOC breakdown (see fig. 8).|[0059] This study demonstrates that increasing soil depth significantly alters the soil microbial community characteristics by reducing the carbon degradation functional gene markers and enzyme activity, thereby reducing the rate of SOC decomposition and weakening the soil carbon release process. The research results show that in tea garden management, the adoption of deep-ploughing cultivation assisted with the fertilization system of pruning residues and returning to the field has urgent need for improving the SOC storage capacity.|[0060] Comparative example 1|The difference from example 1 is that the deep-ploughing depth is 70 cm, the surface soil is 0-20 cm, and the deep soil is 20-70 cm.|[0061] The results show that the physical channel for downward transport of the carbon source is blocked due to insufficient deep-drawing depth. It is directly expressed that the SOC mineralization amount of 80-100 cm soil layers is increased to 338 mg/kg, and the carbon fixation efficiency is reduced by 11.9% compared with that of the embodiment 1 (302 mg/kg). The result shows that the deep-turning depth reaching 80-100 cm and the division modes of the surface layer and the deep soil are necessary means for realizing the expected carbon fixing effect.|[0062] Comparative example 2|The difference from example 1 is that only 6000 kg/ha of organic fertilizer was applied in the deep soil without the addition of clippings.|[0063] The results indicate that, although organic fertilizers provide a stable carbon source, the deep microbial community cannot be activated rapidly due to the lack of readily decomposable carbon components contained in the prune fragments. The method is directly characterized in that the mineralization amount of SOC is increased to 360 mg/kg, the carbon fixation efficiency is reduced by about 19.2% compared with that of the embodiment 1, and meanwhile, the initial colonization and the abundance increase of key carbon circulation functional flora such as Alphaproteobacteria are also obviously delayed. Therefore, the synergistic effect generated by the mixed application of the pruning and the organic fertilizer in deep soil is a key for realizing quick start and maintaining long-term high-efficiency carbon fixation.|[0064] The above examples illustrate only a few embodiments of the invention, which are described in detail and are not to be construed as limiting the scope of the invention. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the invention, which are all within the scope of the invention. Accordingly, the scope of protection of the present invention is to be determined by the appended claims. Family Number|(117150097)|117150097|Abstract|(CN121176213 A)|The invention provides a tea garden soil organic carbon improving method based on deep ploughing and trimmed object returning , and relates to the technical field of soil remediation . The tea garden soil organic carbon improving method based on deep ploughing and trimmed object returning comprises the following steps that S1 , tea garden soil is layered , the soil is deeply ploughed to 80-100 cm , and a soil layer is divided into a soil surface layer and a soil deep layer ; s2 , pruning tea trees after tea picking , and crushing pruned objects to 2-5 cm to obtain pruned object fragments ; s3 , applying compound fertilizer to the surface layer of the soil , and applying the trimmed object fragments and organic fertilizer in the step S2 to the deep layer of the soil ; s4 , performing water management on the soil through micro - spray irrigation to improve organic carbon in the soil of the tea garden . According to the method , deep ploughing and returning of pruned objects to the field are combined , the carbon sequestration capacity of the tea garden soil is remarkably improved , the deep SOC mineralization rate is reduced , the residence time of carbon in the soil is prolonged , the overall carbon sequestration efficiency is improved , the microbial community structure is optimized , the gene abundance related to carbon decomposition in the deep soil is reduced , and the resource utilization rate is increased . |CPC codes|(CN121176213 A)|A01B - 079/02 |IPC codes|(CN121176213 A)|A01B - 079/02 | Other special machines A01B-079/02 A01B-079/02 A01B-079/02 A01B-079/02 PENDING (CN121176213)|PENDING ALIVE (CN121176213)|ALIVE (CN121176213)|LEGAL DETAILS FOR CN121176213|Actual or expected expiration date=2045-11-18|Legal state=ALIVE|Status=PENDING|Event publication date=2025-11-18|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511686192|Application date=2025-11-18|Standardized application number=2025CN-1686192|Event publication date=2025-12-23|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121176213|Publication stage code=A|Publication date=2025-12-23|Standardized publication number=CN121176213|Event publication date=2025-12-23|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2026-01-09|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121176213)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfKDmt8tLvX41fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080161622&ekey=2171&xpn=CN121176213&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=clYqsd6CqewxFJu6HM2YLpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121176213)|CN (CN121176213)|NAME=TEA RESEARCH INSTITUTE CHINESE ACADEMY OF AGRICULTURAL SCIENCES , COUNTRY=CN (CN121176213)|NAME=ZHANG XU;BEIJING XINRUISEN INTELLECTUAL PROPERTY AGENCY CO., LTD. , REG=11961 (CN121176213)|CN (CN121176213)|NAME=ZHANG SHAOBO, COUNTRY=CN |NAME=LI XIN|NAME=ZHANG LAN|NAME=YAN PENG|NAME=ZHANG HONGBIN|NAME=HUANG SHUPING 0 1 Titre: (CN121176213)|Tea garden soil organic carbon improving method based on deep ploughing and trimmed object returning to field Résumé: (CN121176213)|The invention provides a tea garden soil organic carbon improving method based on deep ploughing and trimmed object returning, and relates to the technical field of soil remediation. The tea garden soil organic carbon improving method based on deep ploughing and trimmed object returning comprises the following steps that S1, tea garden soil is layered, the soil is deeply ploughed to 80-100 cm, and a soil layer is divided into a soil surface layer and a soil deep layer; s2, pruning tea trees after tea picking, and crushing pruned objects to 2-5 cm to obtain pruned object fragments; s3, applying compound fertilizer to the surface layer of the soil, and applying the trimmed object fragments and organic fertilizer in the step S2 to the deep layer of the soil; s4, performing water management on the soil through micro-spray irrigation to improve organic carbon in the soil of the tea garden. According to the method, deep ploughing and returning of pruned objects to the field are combined, the carbon sequestration capacity of the tea garden soil is remarkably improved, the deep SOC mineralization rate is reduced, the residence time of carbon in the soil is prolonged, the overall carbon sequestration efficiency is improved, the microbial community structure is optimized, the gene abundance related to carbon decomposition in the deep soil is reduced, and the resource utilization rate is increased. 74 Abstract gpt-4o-mini no The article focuses on improving soil organic carbon in tea gardens through deep ploughing and returning pruned materials, without addressing mineral weathering or CO₂ capture.
75 CN202110411481 CN202110411481 CN113511654|CN113511654 96539972 CN113511654 B 2022-11-15 [CN113511654B]|CN113511654 A 2021-10-19 [CN113511654] 2021-04-16 2021-04-16 2022-11-15|2021-10-19 (CN113511654B)|2022-11-15 (CN113511654)|2041-04-16 (CN113511654)|Capacitance carbon and preparation method thereof (CN113511654)|The invention relates to capacitor carbon and a preparation method thereof, and relates to the technical field of capacitor carbon. According to the main technical scheme, the preparation method of the capacitance carbon comprises the following steps: a pretreatment source tempering step: carrying out pretreatment tempering treatment on a biomass raw material to obtain the biomass raw material subjected to tempering treatment; wherein the pretreatment tempering treatment comprises the steps of conducting crushing, sieving, pickling, water washing and drying on the biomass raw material; a low-temperature carbon sequestration step: carrying out pre-oxidation treatment on the biomass raw material subjected to thermal refining treatment to obtain a pre-oxidation product; a carbonization step: carrying out carbonization treatment on the pre-oxidized product to obtain a carbonized product; and an activation step: performing activation treatment on the carbonized product to obtain the capacitor carbon. According to the method, after the pretreatment source tempering process and the low-temperature carbon sequestration process are added, the purity of the capacitor carbon is improved, the performance is optimized, and meanwhile, the yield of the capacitor carbon is also greatly improved. INSTITUTE OF COAL CHEMISTRY - CHINESE ACADEMY OF SCIENCE (CN113511654)|SHANXI INSTITUTE OF COAL CHEMISTRY CHINESE ACADEMY OF SCIENCES ([CN])|(CN113511654)|SHANXI INSTITUTE OF COAL CHEMISTRY CHINESE ACADEMY OF SCIENCES ([CN]) YUAN SHUXIA|ZHOU JINGJIE (CN113511654)|YUAN SHUXIA|ZHOU JINGJIE|(CN113511654)|YUAN SHUXIA|ZHOU JINGJIE (CN113511654)|LIANG YONGFANG;BEIJING XURUN LAW FIRM|Reg. Nb: 11522 (CN113511654)|Compared with the prior art, the process provided by the invention has the advantages that the performance of the capacitance carbon material is optimized, the purity is improved and the yield of the capacitance carbon is greatly improved after the pretreatment source quenching and tempering process and the low-temperature carbon fixation process are additionally arranged.|The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical solutions of the present invention more clearly understood and to make the technical solutions of the present invention practical in accordance with the contents of the specification, the following detailed description is given of preferred embodiments of the present invention with reference to the accompanying drawings.|Compared with the traditional fossil fuel, the biomass raw material has the disadvantages of low bulk density and energy density, high water content, strong hygroscopicity (hydrophilicity), difficult grinding, poor liquidity and the like; these disadvantages pose challenges and problems to the biomass thermochemical conversion and treatment process: (1) The low bulk density is detrimental to the storage and transportation of the biomass feedstock, resulting in increased costs for storage and transportation of the biomass feedstock.|In addition, the defects of high water content, irregular particle size and shape distribution, low bulk density and the like of the biomass raw material cause poor fluidity of the biomass raw material, and further cause the failure of a biomass raw material feeding system, which is a main factor for limiting the further amplification of the industrial utilization scale of the biomass.| (CN113511654)|1. The preparation method of the capacitance carbon is characterized by comprising the following steps:pretreating a source to temper: carrying out pretreatment and tempering on the biomass raw material to obtain a tempered biomass raw material; wherein the pretreatment quenching and tempering treatment comprises the steps of crushing, screening, acid washing, water washing and drying the biomass raw material; wherein the biomass material is corn leaves; sieving the crushed biomass raw material through a 40-200 mesh sieve; in the step of the acid washing treatment: the adopted acid solution comprises one or more of hydrochloric acid, nitric acid and sulfuric acid; washing the biomass raw material subjected to acid washing with deionized water until the biomass raw material is neutral;and (3) low-temperature carbon fixation: carrying out pre-oxidation treatment on the biomass raw material after the quenching and tempering treatment to obtain a pre-oxidation product; heating the biomass raw material subjected to thermal refining treatment to a pre-oxidation treatment temperature in an air or oxygen atmosphere, and performing pre-oxidation treatment; wherein the pre-oxidation treatment temperature is 100-350 ℃, and the pre-oxidation treatment time is 0.5-10h; the low-temperature carbon fixation step stabilizes a carbon skeleton through pre-oxidation, prevents carbon elements from escaping as carbon-containing gas micromolecules, and reduces the generation of liquid products, thereby reducing the loss of the carbon elements;a carbonization step: carbonizing the pre-oxidized product to obtain a carbonized product;an activation step: activating the carbonized product to obtain capacitance carbon; soaking the carbonized product and an activating agent in deionized water according to a set mass ratio for soaking treatment; drying the product after the dipping treatment; then, under the protective atmosphere, heating the product of the dipping treatment to an activation temperature for activation treatment, cooling to room temperature, and washing with water to be neutral to obtain capacitance carbon; the activation temperature is 300-1000 ℃, and the activation treatment time is 0.5-10h;wherein the yield of the capacitance carbon prepared by the preparation method of the capacitance carbon is 25-40%.| (CN113511654)|In view of this, the present invention provides a capacitance carbon and a preparation method thereof, and mainly aims to improve the performance, purity and yield of a capacitance carbon material. In order to achieve the purpose, the invention mainly provides the following technical scheme: in one aspect, an embodiment of the present invention provides a method for preparing capacitance carbon, including the following steps:|The invention relates to capacitance carbon and a preparation method thereof, and relates to the technical field of capacitance carbon.|The invention relates to the technical field of capacitance carbon, in particular to capacitance carbon and a preparation method thereof.| (CN113511654)|CAPACITANCE CARBON(100,70)|BIOMASS FEEDSTOCK TRANSPORTATION(100,2)|BIOMASS FEEDSTOCK(74,3)|BIOMASS THERMOCHEMICAL CONVERSION(60,1)|PRETREATMENT QUENCHING(57,3)|PRODUCING CAPACITIVE CARBON(56,12)|TEMPERING TREATMENT(51,6)|CARBONIZED PRODUCT(47,15)|PREOXIDATION PRODUCT(45,8)|UTILIZATION AMPLIFICATION(42,1)|CAPACITANCE CARBON YIELD(41,5)|PREOXIDATION TREATMENT(38,9)|POSE CHALLENGE(38,1)|DIPPING TREATMENT(37,8)|PRETREATMENT TEMPERING(37,1)|PRETREATMENT SOURCE QUENCHING(35,3)|REFINING TREATMENT(34,4)|BIOMASS RAW MATERIAL(31,66)|PREOXIDATION TREATMENT TEMPERATURE(29,14)|PREOXIDIZED PRODUCT(29,4)|CAPACITANCE CARBON PURITY(29,1)|CARBON CAPACITY(28,5)|ACIDIC WASH(27,9)|MESH SIEVE(27,2)|SOAKING TREATMENT(26,2)|QUENCHING(25,3)|CAPACITANCE CARBON CYCLING STABILITY(25,1)|TEMPERED BIOMASS RAW MATERIAL(24,2)|PRECONDITIONING SOURCE CONDITIONING(24,1)|CORN LEAVE(23,15)|CARBONIZATION(23,14)|ACTIVATION TREATMENT(23,7)|HYGROSCOPICITY(23,1)|GAS MICROMOLECULE(22,4)|PRETREATMENT SOURCE TEMPERING(22,2)|HYDROPHILICITY(22,1)|CARBON FIXATION(21,22)|CRUSHING(21,4)|DIFFICULT GRINDING(21,1)|PICKLING TREATMENT(21,1)|CARBONIZATION TEMPERATURE(20,17)|ACTIVATION TEMPERATURE(20,13)|SCREENING(20,3)|PREOXIDIZED CORN LEAVE(19,6)|OXYGEN ATMOSPHERE(19,3)|TEMPERING(19,2)|CARBONIZED CORN LEAVE(18,7)|PREOXIDATION(18,4)|BULK DENSITY(18,3)|ADOPTED ACID SOLUTION(18,2)|TEMPERING(18,2)|BIOMASS RAW MATERIAL FLUIDITY(18,1)|CRUSHED BIOMASS RAW MATERIAL(18,1)|ACIDIC WASHING TREATMENT(17,4)|IMPREGNATION TREATMENT(17,3)|CAPACITANCE CARBON PERFORMANCE(17,2)|LIQUID(17,2)|PURITY(16,5)|PREOXIDATION PRODUCT HEATING(16,2)|FOSSIL FUEL(16,1)|IMPREGNATED PRODUCT(16,1)|PROTECTIVE ATMOSPHERE(15,8)|PRETREATING(15,6)|BIOMASS(14,3)|DISCHARGE SPECIFIC CAPACITANCE(13,4)|CHARRING TEMPERATURE(13,2)|BIOMASS RAW MATERIAL FEEDING(13,1)|ACTIVATION(12,21)|HEATING RATE(12,15)|CARBON SKELETON(11,3)|ACIDIC SOLUTION(10,8)|CAPACITANCE CARBON MATERIAL(10,7)|CRUSHED CORN LEAVE(10,3)|INCREASED COST(10,1)|DEIONIZED WATER(9,14)|LIQUID PRODUCT(9,4)|SHAPE DISTRIBUTION(9,4)|SOAKED CORN LEAVE(9,2)|NITROGEN ATMOSPHERE(8,6)|ALCL(8,4)|ZNCL(8,4)|IRREGULAR PARTICLE SIZE(8,3)|TEMPERED CORN(8,3)|CARBON FIXATION(8,1)|CARBON(7,6)|HYDROCHLORIC ACID(7,6)|SULFURIC ACID(7,5)|NAOH(7,4)|NITRIC ACID(7,4)|CAPACITANCE CARBON MATERIAL PERFORMANCE(7,2)|GENERAL APPLICABILITY(7,2)|BIOMASS MATERIAL(7,1)|PREOXIDATION TREATMENT TIME(6,6)|PREOXIDATION TEMPERATURE(6,4)|TUBULAR FURNACE(6,4)|WASHED BIOMASS RAW MATERIAL(6,3)|ENERGY DENSITY(6,2)|BIOMASS CAPACITIVE CARBON(6,1)|BIOMASS THERMODYNAMIC(6,1)|CAPACITANCE CARBON COMMERCIALIZATION REQUIREMENT(6,1)|COMMERCIALIZED CAPACITANCE CARBON REQUIREMENT(6,1)|SUPERCAPACITOR INDUSTRY DEVELOPMENT(6,1)|ROOM TEMPERATURE(5,6)|ACTIVATION TREATMENT TIME(5,5)|REFINING(5,4)|CARRYING OUT PREOXIDATION(5,2)|CAPACITOR CYCLING STABILITY(5,1)|CARBON FIXING(5,1)|SCIENTIFIC SIGNIFICANCE(5,1)|SUPERCAPACITOR CYCLE STABILITY(5,1)|ULTRAHIGH PURITY(5,1)|WASHED CORN LEAVE(5,1)|CARBONIZATION TREATMENT TIME(4,5)|CAPACITOR CARBON(4,3)|NEUTRALITY(4,3)|PYROLYSIS PRODUCT(4,3)|SIEVING(4,3)|CAPACITANCE CARBON ORGANIC SYSTEM(4,2)|CARBON ESCAPE(4,2)|PRETREATMENT SOURCE CONDITIONING(4,2)|PYROLYSIS REACTION(4,2)|SOAKING TIME(4,2)|STACKING DENSITY(4,2)|BIOMASS PARTICLE(4,1)|COMPACTION DENSITY(4,1)|FRUIT SHELL(4,1)|HIGH WATER CONTENT DEFECT(4,1)|MODIFIED CORN LEAF(4,1)|SUPERCAPACITOR PERFORMANCE(4,1)|LOW TEMPERATURE CARBON FIXATION(3,19)|0F G(3,4)|SET MASS RATIO(3,4)|CARRYING OUT PRETREATMENT(3,3)|INVESTMENT(3,2)|RICE HULL(3,2)|BIOMASS DIFFERENCE(3,1)|CAPACITANCE RATIO(3,1)|COMPETITIVE RELATIONSHIP(3,1)|ELECTROCHEMICAL PERFORMANCE(3,1)|EQUIPMENT PRODUCTIVITY(3,1)|MATERIALTHE EQUIVALENT SERIES(3,1)|MODIFIED CORN LEAVE(3,1)|PHYSICOCHEMICAL PROPERTY STABILITY(3,1)|PRODUCT OVERHIGH OXYGEN CONTENT(3,1)||(CN113511654)|CAPACITANCE CARBON(100,68)|BIOMASS FEEDSTOCK TRANSPORTATION(100,2)|BIOMASS FEEDSTOCK(67,2)|BIOMASS THERMOCHEMICAL CONVERSION(60,1)|PRETREATMENT QUENCHING(57,3)|TEMPERING TREATMENT(51,6)|PREOXIDATION PRODUCT(45,8)|CARBONIZED PRODUCT(43,15)|PRODUCING CAPACITIVE CARBON(43,7)|UTILIZATION AMPLIFICATION(42,1)|POSE CHALLENGE(38,1)|PRETREATMENT TEMPERING(37,1)|PRETREATMENT SOURCE QUENCHING(35,3)|PRETREATMENT SOURCE TEMPERING(32,3)|BIOMASS RAW MATERIAL(30,67)|ALCL3AND H3PO4ONE(30,2)|PREOXIDIZED PRODUCT(29,4)|CAPACITANCE CARBON PURITY(29,1)|CAPACITANCE CARBON YIELD(28,4)|ACTIVATION TREATMENT(27,8)|DIPPING TREATMENT(27,8)|CARBON CAPACITY(27,5)|IMPREGNATION TREATMENT(25,4)|QUENCHING(25,3)|CAPACITANCE CARBON CYCLING STABILITY(25,1)|PRECONDITIONING SOURCE CONDITIONING(24,1)|CARBONIZATION(23,15)|PREOXIDATION TREATMENT TEMPERATURE(23,14)|ACIDIC WASH(23,9)|HYGROSCOPICITY(23,1)|HYDROPHILICITY(22,1)|CRUSHING(21,4)|DIFFICULT GRINDING(21,1)|CARBONIZATION TEMPERATURE(20,17)|SCREENING(20,3)|TEMPERED BIOMASS RAW MATERIAL(20,3)|CARBON FIXATION(19,23)|PREOXIDIZED CORN LEAVE(19,6)|CAPACITIVE CARBON YIELD(19,1)|CARBONIZED CORN LEAVE(18,7)|BULK DENSITY(18,3)|FRUIT SHELL(18,2)|TEMPERING(18,2)|BIOMASS RAW MATERIAL FLUIDITY(18,1)|REFINING TREATMENT(17,3)|TEMPERING(17,3)|CAPACITANCE CARBON PERFORMANCE(17,2)|LIQUID(17,2)|ACIDIC WASHING TREATMENT(16,5)|PURITY(16,5)|PREOXIDATION PRODUCT HEATING(16,2)|SOAKING TREATMENT(16,2)|FOSSIL FUEL(16,1)|PRETREATING(15,6)|ACTIVATION TEMPERATURE(14,13)|BIOMASS(14,3)|PROTECTIVE ATMOSPHERE(13,8)|DISCHARGE SPECIFIC CAPACITANCE(13,4)|CHARRING TEMPERATURE(13,2)|BIOMASS RAW MATERIAL FEEDING(13,1)|ACTIVATION(12,22)|HEATING RATE(12,17)|OXYGEN ATMOSPHERE(12,3)|ADOPTED ACID SOLUTION(11,2)|ACIDIC SOLUTION(10,8)|CAPACITANCE CARBON MATERIAL(10,7)|CRUSHED CORN LEAVE(10,3)|RICE HULL(10,3)|CARBON FIXATION(10,2)|INCREASED COST(10,1)|SHAPE DISTRIBUTION(9,4)|NITROGEN ATMOSPHERE(8,6)|NA2CO3(8,4)|ZNCL2(8,4)|IRREGULAR PARTICLE SIZE(8,3)|SIEVE(8,3)|STRAW(8,3)|TEMPERED CORN(8,3)|NAOH(7,4)|CAPACITANCE CARBON MATERIAL PERFORMANCE(7,2)|GENERAL APPLICABILITY(7,2)|DEIONIZED WATER(6,14)|PREOXIDATION TEMPERATURE(6,4)|TUBULAR FURNACE(6,4)|WASHED BIOMASS RAW MATERIAL(6,3)|ENERGY DENSITY(6,2)|BIOMASS CAPACITIVE CARBON(6,1)|BIOMASS THERMODYNAMIC(6,1)|CAPACITANCE CARBON COMMERCIALIZATION REQUIREMENT(6,1)|COMMERCIALIZED CAPACITANCE CARBON REQUIREMENT(6,1)|SOAKED CORN LEAVE(6,1)|SUPERCAPACITOR INDUSTRY DEVELOPMENT(6,1)|NITRIC ACID(5,4)|GAS MICROMOLECULE(5,3)|CARRYING OUT PREOXIDATION(5,2)|CAPACITOR CYCLING STABILITY(5,1)|CARBON CO2THE ESCAPE(5,1)|SCIENTIFIC SIGNIFICANCE(5,1)|SUPERCAPACITOR CYCLE STABILITY(5,1)|ULTRAHIGH PURITY(5,1)|WASHED CORN LEAVE(5,1)|PREOXIDATION TREATMENT TIME(4,6)|ROOM TEMPERATURE(4,6)|CARBONIZATION TREATMENT TIME(4,5)|CAPACITOR CARBON(4,3)|NEUTRALITY(4,3)|PYROLYSIS PRODUCT(4,3)|SIEVING(4,3)|CAPACITANCE CARBON ORGANIC SYSTEM(4,2)|PRETREATMENT SOURCE CONDITIONING(4,2)|PYROLYSIS REACTION(4,2)|SOAKING TIME(4,2)|STACKING DENSITY(4,2)|BIOMASS PARTICLE(4,1)|COMPACTION DENSITY(4,1)|HIGH WATER CONTENT DEFECT(4,1)|MODIFIED CORN LEAF(4,1)|SUPERCAPACITOR PERFORMANCE(4,1)|ACTIVATION TREATMENT TIME(3,5)|0F G(3,4)|CARRYING OUT PRETREATMENT(3,3)|INVESTMENT(3,2)|BIOMASS DIFFERENCE(3,1)|CAPACITANCE RATIO(3,1)|CARBON ESCAPE(3,1)|COMPETITIVE RELATIONSHIP(3,1)|ELECTROCHEMICAL PERFORMANCE(3,1)|EQUIPMENT PRODUCTIVITY(3,1)|IMMERSION TREATMENT(3,1)|PHYSICOCHEMICAL PROPERTY STABILITY(3,1)|PRODUCT OVERHIGH OXYGEN CONTENT(3,1)|TAP DENSITY(3,1)|ARGON(2,3)| (CN113511654)|1. The preparation method of the capacitance carbon is characterized by comprising the following steps:|pretreating a source to temper: carrying out pretreatment and tempering on the biomass raw material to obtain a tempered biomass raw material; wherein the pretreatment quenching and tempering treatment comprises the steps of crushing, screening, acid washing, water washing and drying the biomass raw material; wherein the biomass material is corn leaves; sieving the crushed biomass raw material through a 40-200 mesh sieve; in the step of the acid washing treatment: the adopted acid solution comprises one or more of hydrochloric acid, nitric acid and sulfuric acid; washing the biomass raw material subjected to acid washing with deionized water until the biomass raw material is neutral;|and (3) low-temperature carbon fixation: carrying out pre-oxidation treatment on the biomass raw material after the quenching and tempering treatment to obtain a pre-oxidation product; heating the biomass raw material subjected to thermal refining treatment to a pre-oxidation treatment temperature in an air or oxygen atmosphere, and performing pre-oxidation treatment; wherein the pre-oxidation treatment temperature is 100-350 ℃, and the pre-oxidation treatment time is 0.5-10h; the low-temperature carbon fixation step stabilizes a carbon skeleton through pre-oxidation, prevents carbon elements from escaping as carbon-containing gas micromolecules, and reduces the generation of liquid products, thereby reducing the loss of the carbon elements;|a carbonization step: carbonizing the pre-oxidized product to obtain a carbonized product;|an activation step: activating the carbonized product to obtain capacitance carbon; soaking the carbonized product and an activating agent in deionized water according to a set mass ratio for soaking treatment; drying the product after the dipping treatment; then, under the protective atmosphere, heating the product of the dipping treatment to an activation temperature for activation treatment, cooling to room temperature, and washing with water to be neutral to obtain capacitance carbon; the activation temperature is 300-1000 ℃, and the activation treatment time is 0.5-10h;|wherein the yield of the capacitance carbon prepared by the preparation method of the capacitance carbon is 25-40%.|2. The process for producing capacitive carbon according to claim 1,|the concentration of the acid solution is 0.1-5mol/L.|3. The process for producing capacitive carbon according to claim 1,|the pickling treatment comprises the following specific steps: the biomass feedstock is soaked in the acid solution.|4. The method of producing capacitive carbon according to claim 3,|the soaking time is 0.1-24h.|5. The process for producing capacitive carbon according to claim 1,|before the step of conditioning the pretreatment source, the method further comprises the following steps: and cleaning and drying the biomass raw material.|6. The method of making capacitive carbon of claim 1, wherein in the preconditioning source conditioning step:|and drying the washed biomass raw material at the temperature of 60-90 ℃ for 2-15h.|7. The method for preparing capacitive carbon according to claim 1, wherein in the low-temperature carbon fixation step:|in the process of heating the biomass raw material after the thermal refining treatment to the pre-oxidation treatment temperature: the heating rate is 0.1-20 ℃/min.|8. The method for producing capacitive carbon according to claim 1, wherein in the carbonizing step:|and heating the pre-oxidized product to a carbonization temperature under a protective atmosphere, carrying out carbonization treatment, and cooling to room temperature to obtain a carbonized product.|9. The method of producing capacitive carbon according to claim 8,|the carbonization temperature is 400-1000 ℃, and the carbonization treatment time is 0.5-10h.|10. The method of producing capacitive carbon according to claim 8,|during the heating of the pre-oxidation product to the charring temperature: the heating rate is 0.1-20 deg.C/min.|11. The method of producing capacitive carbon according to claim 8,|after the pre-oxidation treatment in the low-temperature carbon fixation step is finished, the atmosphere is switched to a protective atmosphere, and the pre-oxidation product is heated to the carbonization temperature from the pre-oxidation treatment temperature.|12. The process for producing capacitive carbon according to claim 1,|during the heating of the impregnated product to the activation temperature: the heating rate is 0.1-20 deg.C/min.|13. The method of producing capacitive carbon according to claim 1,|the activating agent is KOH, naOH or K 2 CO 3 、Na 2 CO 3 、ZnCl 2 、AlCl 3 And H 3 PO 4 One or more of them.|14. The process for producing capacitive carbon according to claim 1,|in the step of the impregnation treatment: the set mass ratio is 1: (0.1-100).|15. The method of producing capacitive carbon according to claim 1,|the time of the dipping treatment is 0.5-24h.|16. The capacitance carbon is characterized in that the first discharge specific capacitance of an organic system of the capacitance carbon is more than or equal to 35.0F/g; the first discharge specific capacitance of the inorganic system of the capacitance carbon is more than or equal to 65.0F/g; the cycling stability of the capacitance carbon is more than or equal to 98 percent;|wherein the capacitance carbon is prepared by the preparation method of the capacitance carbon as claimed in any one of claims 1 to 15.|17. The capacitive carbon of claim 16,|the content of metallic elements, namely iron element, is not more than 50mg/kg, the content of nickel element is not more than 50mg/kg, the content of cobalt element is not more than 20mg/kg, the content of copper element is not more than 20mg/kg, the content of sodium element is not more than 100mg/kg, the content of potassium element is not more than 200mg/kg, and the content of aluminum element is not more than 200mg/kg. (CN113511654)|TECHNICAL FIELD|[0001] The invention relates to the technical field of capacitance carbon, in particular to capacitance carbon and a preparation method thereof.|BACKGROUND ART|[0002] The super capacitor has the characteristics of high power, long service life, wide use temperature and the like, and has wide application prospect in the fields of electric vehicles, smart grids, portable electronic equipment and the like.|[0003] The porous carbon material has the characteristics of good conductivity, large specific surface area, stable physicochemical property, rich pore structure and the like, and becomes the electrode material of the super capacitor which is widely researched at present. The commercial super capacitor has very strict requirements on various indexes of the carbon-based electrode material, including ultrahigh purity, large specific surface area, porous structure, high conductivity, high compaction density, low cost and the like, and more than 90% of the carbon material depends on import at present. How to prepare the low-cost and high-performance capacitance carbon material becomes the difficult problem of 'neck' puzzling the development of the super capacitor industry in China.|[0004] At present, the method for preparing capacitance carbon by biomass is to directly carry out carbonization and activation treatment on biomass raw materials to prepare the capacitance carbon. However, the inventor of the invention finds that the existing method has the technical problems of more investment, less output, low yield and poor performance, and cannot meet the requirement of commercialized capacitance carbon.|DISCLOSURE|Disclosure of Invention|[0005] In view of this, the present invention provides a capacitance carbon and a preparation method thereof, and mainly aims to improve the performance, purity and yield of a capacitance carbon material.|[0006] In order to achieve the purpose, the invention mainly provides the following technical scheme:|[0007] in one aspect, an embodiment of the present invention provides a method for preparing capacitance carbon, including the following steps:|[0008] pretreating a source to temper: carrying out pretreatment and thermal refining on the biomass raw material to obtain a thermal-refined biomass raw material; wherein the pretreatment quenching and tempering treatment comprises the steps of crushing, screening, acid washing, water washing and drying the biomass raw material;|[0009] and (3) low-temperature carbon fixation: carrying out pre-oxidation treatment on the biomass raw material after the quenching and tempering treatment to obtain a pre-oxidation product;|[0010] a carbonization step: carbonizing the pre-oxidized product to obtain a carbonized product;|[0011] an activation step: and carrying out activation treatment on the carbonized product to obtain the capacitance carbon.|[0012] Preferably, in the step of the acid washing treatment: the adopted acid solution comprises one or more of hydrochloric acid, nitric acid and sulfuric acid; preferably, the concentration of the acid solution is 0.1-5mol/L; preferably, the step of acid washing treatment specifically comprises: soaking a biomass raw material in the acid solution; preferably, the soaking time is 0.1-24h.|[0013] Preferably, before the step of conditioning the pretreatment source, the method further comprises: and cleaning and drying the biomass raw material.|[0014] Preferably, in the step of conditioning the pretreatment source: the biomass raw material after being crushed is sieved by a sieve with 40 to 200 meshes.|[0015] Preferably, in the step of conditioning the pretreatment source: and washing the biomass raw material subjected to acid washing with deionized water until the biomass raw material is neutral.|[0016] Preferably, in the step of conditioning the pretreatment source: and drying the washed biomass raw material at the temperature of 60-90 ℃ for 2-15h.|[0017] In the low-temperature carbon fixation step: heating the biomass raw material subjected to thermal refining treatment to a pre-oxidation treatment temperature in an air or oxygen atmosphere, and performing pre-oxidation treatment; preferably, the pre-oxidation treatment temperature is 100-350 ℃, and the pre-oxidation treatment time is 0.5-10h; preferably, in the process of heating the biomass raw material after the thermal refining to the pre-oxidation treatment temperature: the heating rate is 0.1-20 deg.C/min.|[0018] In the carbonization step: under the protective atmosphere (nitrogen or argon), heating the pre-oxidized product to a carbonization temperature, carrying out carbonization treatment, and cooling to room temperature to obtain a carbonized product; preferably, the carbonization temperature is 400-1000 ℃, and the carbonization treatment time is 0.5-10h; preferably, during the heating of the pre-oxidation product to the charring temperature: the heating rate is 0.1-20 ℃/min; preferably, after the pre-oxidation treatment in the low-temperature carbon fixation step is finished, the atmosphere is switched to a protective atmosphere, and the pre-oxidation product is heated from the pre-oxidation treatment temperature to the carbonization temperature.|[0019] Preferably, in the activation step: soaking the carbonized product and an activating agent in deionized water according to a set mass ratio for soaking treatment; drying the product after the dipping treatment; and then, heating the product of the dipping treatment to an activation temperature for activation treatment under a protective atmosphere, cooling to room temperature, and washing with water to be neutral to obtain the capacitance carbon. Preferably, the activation temperature is 300-1000 ℃, and the activation treatment time is 0.5-10h; preferably, during heating of the product of the impregnation treatment to the activation temperature: the heating rate is 0.1-20 ℃/min; preferably, the activating agent is KOH, naOH or K 2 CO 3 、Na 2 CO 3 、ZnCl 2 、AlCl 3 And H 3 PO 4 One or more of the above; preferably, in the step of the impregnation treatment: the set mass ratio is 1: (0.1-100). Preferably, the time of the dipping treatment is 0.5 to 24 hours.|[0020] Preferably, the biomass raw material is any one of corn leaves, straws, rice hulls and fruit shells.|[0021] Preferably, the yield of the capacitance carbon prepared by the preparation method of the capacitance carbon is 25-40%.|[0022] In another aspect, an embodiment of the present invention provides a capacitor carbon; wherein the first discharge specific capacitance of the organic system of the capacitance carbon is more than or equal to 35.0F/g; the first discharge specific capacitance of the inorganic system of the capacitance carbon is more than or equal to 65.0F/g; preferably, the cycling stability (the specific capacity retention rate of the capacitance carbon) of the capacitance carbon is more than or equal to 98 percent;|[0023] preferably, the content of metallic elements, namely iron element, in the capacitance carbon is not more than 50mg/kg, the content of nickel element is not more than 50mg/kg, the content of cobalt element is not more than 20mg/kg, the content of copper element is not more than 20mg/kg, the content of sodium element is not more than 100mg/kg, the content of potassium element is not more than 200mg/kg, and the content of aluminum element is not more than 200mg/kg;|[0024] preferably, the capacitance carbon is prepared by the preparation method of any one of the above methods.|[0025] Compared with the prior art, the capacitance carbon and the preparation method thereof have the following beneficial effects:|[0026] the preparation method of the capacitance carbon provided by the embodiment of the invention adopts the treatment technologies of crushing, sieving, acid washing, water washing to neutrality and drying to carry out pretreatment source conditioning on the biomass raw material, solves the problems of high water content, more impurities, irregular particle size and shape distribution, low stacking density, low equipment utilization rate, poor product stability and the like of the biomass raw material, improves the process consistency of the raw material, and is coupled with the subsequent low-temperature carbon fixation-carbonization-activation process technology to prepare the capacitance carbon material with high yield, reasonable particle size distribution, high purity and high specific capacitance. The invention adds a preoxidation process to stabilize the carbon skeleton to prevent carbon elements from being CO and CO 2 The escape of carbon-containing gas micromolecules and the reduction of the generation of liquid products reduce the loss of carbon elements, the yield of solid carbon is improved by 5-20 percent compared with the traditional process, the production cost is reduced, and meanwhile, the addition of the pre-oxidation process does not cause the result of overhigh oxygen content of the product; therefore, thisThe low-temperature carbon fixation technology has important significance for the large-scale production of the biomass-based capacitance carbon material.|[0027] In conclusion, the preparation method of the capacitance carbon provided by the invention adds a pretreatment source quenching and tempering technology and a low-temperature carbon fixing technology before carbonization, so that the purity of the capacitance carbon material is improved, the performance of the capacitance carbon material is optimized, and meanwhile, the yield of the capacitance carbon is greatly improved.|[0028] The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical solutions of the present invention more clearly understood and to make the technical solutions of the present invention practical in accordance with the contents of the specification, the following detailed description is given of preferred embodiments of the present invention with reference to the accompanying drawings.|DRAWINGS DESCRIPTION|[0029] Fig. 1 is a process flow chart of a method for preparing capacitance carbon provided in example 1 of the present invention.|INVENTION MODE|Detailed Description|[0030] To further explain the technical means and effects of the present invention adopted to achieve the predetermined object, the following detailed description of the embodiments, structures, features and effects according to the present invention will be made with reference to the accompanying drawings and preferred embodiments. In the following description, different "one embodiment" or "an embodiment" refers to not necessarily the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.|[0031] On one hand, the embodiment of the invention provides a preparation method of capacitance carbon, which mainly comprises the following process flows: and (3) carrying out pretreatment source conditioning, low-temperature carbon fixation, carbonization and activation processes on the biomass raw material in sequence to obtain the biomass-based capacitance carbon. The method comprises the following specific steps:|[0032] 1) A cleaning step: and cleaning and drying the biomass raw material.|[0033] 2) Pretreating a source to temper: the biomass raw material is subjected to pretreatment and thermal refining, and the pretreatment and thermal refining specifically comprises crushing, sieving, acid washing, deionized water washing to neutrality and drying treatment.|[0034] The acid solution used in the acid washing treatment is one of hydrochloric acid, nitric acid and sulfuric acid, or the acid solution is a mixed solution of a plurality of acids of hydrochloric acid, nitric acid and sulfuric acid. Preferably, the concentration of the acid solution is 0.1-5mol/L; wherein, the time length of soaking the screened biomass raw material in the acid solution is 0.1-24h.|[0035] Wherein the biomass raw material after being crushed is sieved by a sieve of 40-200 meshes. Here, it is required to pass a 40-200 mesh sieve. The selection of the particle size of the raw material is directly related to the subsequent acid washing, pre-oxidation, carbonization and activation processes, and comprises the determination of the conditions of acid concentration, heating temperature, heat preservation time, heating rate, dipping time and the like. Too small a particle size may result in a reduced char yield. Too large a particle size can result in too large a particle size of the final capacitive carbon product, resulting in a decrease in electrochemical performance.|[0036] And drying the washed biomass raw material at the temperature of 60-90 ℃ for 2-15h.|[0037] 3) And (3) low-temperature carbon fixation: performing low-temperature pre-oxidation treatment on the biomass raw material subjected to the quality treatment in a tubular furnace in the air or oxygen atmosphere; wherein the pre-oxidation treatment temperature is 100-350 ℃, the heating rate is 0.1-20 ℃/min, and the pre-oxidation treatment time is 0.5-10h.|[0038] 4) A carbonization step: and (3) switching the reaction atmosphere to nitrogen or argon, continuously heating to 400-1000 ℃ for carbonization treatment at the heating rate of 0.1-20 ℃/min for 0.5-10h, and then cooling to room temperature to obtain a carbonized product.|[0039] 5) An activation step: and (2) soaking the carbonized product and an activating agent in deionized water according to a preset mass ratio, drying after soaking treatment (preferably, the soaking treatment time is 0.5-24h; the use amount of the deionized water does not exceed the use amount of the carbonized product, so that the carbonized product is uniformly soaked in an activating agent aqueous solution), and then performing activating treatment under a protective atmosphere. The protective atmosphere is nitrogen or argon, the activation temperature is 300-1000 ℃, the heating rate is 0.1-20 ℃/min, and the activation treatment time is 0.5-10h. And then cooling to room temperature, and washing with deionized water to be neutral to obtain the capacitance carbon.|[0040] Wherein the activating agent is KOH, naOH or K 2 CO 3 、Na 2 CO 3 、ZnCl 2 、AlCl 3 And H 3 PO 4 Or the activating agent is KOH, naOH or K 2 CO 3 、Na 2 CO 3 、ZnCl 2 、AlCl 3 And H 3 PO 4 A mixture of a plurality of (a). The preset mass ratio of the carbonized product to the activating agent is 1:0.1-100.|[0041] In the prior art, the method for preparing the capacitance carbon by using the biomass raw material is to directly carbonize and activate the biomass raw material to prepare the capacitance carbon. Compared with the prior art, the preparation process of the capacitive carbon provided by the invention adds two technologies of pretreatment source tempering and low-temperature carbon fixation before the carbonization step, namely the biomass-based capacitive carbon is prepared by adopting a pretreatment source tempering-low Wen Gutan-carbonization-activation process. Compared with the prior art, the process provided by the invention has the advantages that the performance of the capacitance carbon material is optimized, the purity is improved and the yield of the capacitance carbon is greatly improved after the pretreatment source quenching and tempering process and the low-temperature carbon fixation process are additionally arranged. The specific analysis is as follows:|[0042] first, a pretreatment source conditioning technology|[0043] Compared with the traditional fossil fuel, the biomass raw material has the disadvantages of low bulk density and energy density, high water content, strong hygroscopicity (hydrophilicity), difficult grinding, poor liquidity and the like; these disadvantages pose challenges and problems to the biomass thermochemical conversion and treatment process:|[0044] (1) The low bulk density is detrimental to the storage and transportation of the biomass feedstock, resulting in increased costs for storage and transportation of the biomass feedstock. The low energy density limits the overall capacity scale of the biomass thermodynamic system, reducing the economics of the biomass energy source. High water content in the biomass raw material can delay pyrolysis reaction, influence the yield of pyrolysis products and the stability of the products, and increase the heat supply cost. In addition, the defects of high water content, irregular particle size and shape distribution, low bulk density and the like of the biomass raw material cause poor fluidity of the biomass raw material, and further cause the failure of a biomass raw material feeding system, which is a main factor for limiting the further amplification of the industrial utilization scale of the biomass. On the other hand, due to the difference of biomass raw material types and production places, wherein the relative components of hemicellulose, cellulose, lignin and ash are greatly changed, the biomass pyrolysis characteristics and the product distribution are greatly influenced.|[0045] Therefore, the pretreatment source conditioning technology can be used for improving certain physical and chemical properties of the biomass raw materials and is coupled with the subsequent pyrolysis technology, the purpose of maximizing the utilization value of pyrolysis products is achieved, and meanwhile, the difference among different biomass raw materials is reduced due to the use of the technology, so that the technology disclosed by the invention has universal applicability.|[0046] (2) The particle size and the morphology of the raw materials influence the dynamic parameter change (drying, heating rate and reaction rate) of biomass particles and the particle size and the morphology of the final product capacitance carbon material; the particle size distribution and the particle size of the capacitance carbon material influence the specific surface area and the tap density, so that the processing technology and the rate capability of the electrode material are influenced.|[0047] (3) The activated carbon is used as a key electrode material, and the purity of the activated carbon directly determines the performance of the supercapacitor. The metal ions (iron, nickel, cobalt, copper, sodium, potassium, aluminum, etc.) in the activated carbon undergo redox reactions during charging to generate leakage current, thereby causing the voltage of the capacitor to drop. At the same time, the ions also affect the cycling stability of the capacitor, resulting in a reduced lifetime. Therefore, the removal of impurity metal ions and the improvement of the purity of the activated carbon have important significance for improving the performance of the capacitor.|[0048] Aiming at the problems of the biomass raw material, the invention adopts the treatment technologies of crushing, sieving, acid washing, water washing to neutrality and drying to carry out pretreatment source conditioning on the biomass raw material, solves the problems of high water content, more impurities, irregular particle size and shape distribution, low stacking density, low equipment utilization rate, poor product stability and the like of the raw material, improves the process consistency of the raw material, and is coupled with the subsequent low-temperature carbon fixation-carbonization-activation process technology to prepare the capacitance carbon material with high yield, reasonable particle size distribution, high purity and high specific capacitance.|[0049] Here, repeated emphasis is given to: the biomass raw material has the following problems: (1) High water content in the biomass raw material can delay pyrolysis reaction, influence the yield and product stability of pyrolysis products, and increase heat supply cost, so that the raw material is dried; (2) The size and shape distribution of the raw material particles can influence mass transfer and heat transfer of the subsequent process, so that the raw material is crushed and sieved; (3) The relative composition of hemicellulose, cellulose, lignin and ash in the raw material is greatly changed due to the difference of biomass types and production places, the biomass pyrolysis characteristics and the product distribution are greatly influenced, the raw material is purified through acid treatment, the difference among different biomass raw materials is reduced, and the subsequent process has universal applicability. Based on this, through long-term and large-scale experimental research, the particle sizes with different meshes are matched with corresponding processes of low-temperature carbon fixation, carbonization, activation and the like, and the final physical and chemical properties of the target product of the invention can be obtained. "move the whole body by pulling one movement", there is a relationship of correlation and coupling between each process parameter.|[0050] Second, low temperature carbon sequestration|[0051] In the prior art, the problems of more investment, less output and low yield exist in the process of preparing the carbon material by using the biomass. The advantages of low equipment productivity and low raw material cost can be reduced, and the commercialization requirement of the capacitance carbon can not be met. Therefore, the improvement of the carbon yield becomes a core problem of the industrial production of the biomass carbon material.|[0052] The pyrolysis of the biomass raw material can generate gas, liquid and solid three-state products, and carbon elements can be CO and CO 2 And the carbon-containing gas micromolecules, liquid products such as acids, phenols, ketones, alcohols, esters and the like and solid carbon are distributed, and the yield of the three products has a competitive relationship. Based on the method, the low-temperature carbon fixation technology is added to the existing manufacturing process, and the carbon skeleton is stabilized through pre-oxidation to prevent carbon elements from being CO and CO 2 And the escape of carbon-containing gas micromolecules and the reduction of the generation of liquid products reduce the loss of carbon elements, improve the yield of solid carbon by 5-20 percent compared with the traditional process and reduce the production cost. In addition, oxygen-containing functional groups on the surface of the capacitance carbon have strong electrochemical activity and are easy to generate decomposition reaction during charging and discharging, so that the cycle stability of the super capacitor is reduced. At the same time, the oxygen-containing functional groups reduce the materialThe equivalent series internal resistance is increased, and the power density and the cycle life of the capacitor are reduced. Therefore, the method has great scientific significance and application value in controlling the oxygen content of the capacitance carbon material. In the invention, the addition of the low-temperature carbon fixation technology has no consequence of over-high oxygen content of the product. Therefore, the low-temperature carbon fixation technology has important significance for the large-scale production of the biomass-based capacitance carbon material.|[0053] The invention is further illustrated by the following specific experimental examples:|[0054] example 1|[0055] In this example, a capacitance carbon is prepared, as shown in fig. 1, by the following main preparation steps:|[0056] 1) Cleaning and drying the biomass raw material corn leaves.|[0057] 2) Pretreating a source to temper:|[0058] crushing the corn leaves treated in the step 1), sieving the crushed corn leaves with a 60-mesh sieve, then soaking the crushed corn leaves in a proper amount of 1mol/L hydrochloric acid solution, washing the crushed corn leaves with deionized water to be neutral after 12 hours, and drying the washed corn leaves (the drying temperature is 60 ℃ and the drying time is 15 hours) to obtain the corn leaves (namely, the modified corn leaves are powdery) after the modification treatment.|[0059] 3) Low temperature carbon fixation step|[0060] Putting 10g of the tempered corn leaves into a tube furnace for pre-oxidation treatment to obtain pre-oxidized corn leaves; wherein the pre-oxidation treatment temperature is 200 ℃, the pre-oxidation treatment time (namely, the heat preservation time at the pre-oxidation treatment temperature) is 2h, and the heating rate in the process of heating the modified corn leaves to the pre-oxidation treatment temperature is 2 ℃/min.|[0061] 4) Carbonization step|[0062] Carbonizing the pre-oxidized corn leaves in a tubular furnace in nitrogen atmosphere to obtain carbonized corn leaves; wherein the carbonization temperature is 600 ℃, and the carbonization treatment time (the heat preservation time at the carbonization temperature) is 4h; the heating rate in the process of heating the modified corn leaves to the carbonization temperature is 2 ℃/min.|[0063] 5) Step of activation|[0064] Soaking the carbonized corn leaves and KOH in deionized water according to the mass ratio of 1:4 for 12 hours; drying the corn leaves after the dipping treatment, then putting the corn leaves into a tube furnace, and carrying out activation treatment in a nitrogen atmosphere; wherein the activation temperature is 800 ℃, the activation treatment time is 1h, and the temperature rise rate in the process of heating the corn leaves after the dipping treatment to the activation temperature is 2 ℃/min. And after the activation is finished, cooling, taking out, washing with acid and water to be neutral, and drying to obtain the capacitance carbon.|[0065] Example 2|[0066] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0067] in the activation step of this embodiment, the selected activating agent is sodium carbonate, and the carbonized corn leaves and the sodium carbonate are mixed according to a mass ratio of 1:10, and immersing in deionized water for 20 hours.|[0068] The rest steps are completely consistent.|[0069] Example 3|[0070] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0071] pretreating a source to temper: crushing the corn leaves treated in the step 1), sieving the crushed corn leaves with a 60-mesh sieve, then soaking the crushed corn leaves in a proper amount of 0.1mol/L sulfuric acid solution, washing the crushed corn leaves with deionized water to be neutral after 24 hours, and drying the washed corn leaves to obtain the corn leaves subjected to thermal refining (namely, the thermal refining corn leaves are powdery).|[0072] The rest steps are completely consistent.|[0073] Example 4|[0074] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0075] pretreating a source to temper: crushing the corn leaves treated in the step 1), sieving the crushed corn leaves with a 60-mesh sieve, then soaking the crushed corn leaves in a proper amount of 5mol/L hydrochloric acid solution, washing the crushed corn leaves with deionized water to be neutral after 0.1 hour, and drying the washed corn leaves to obtain the corn leaves subjected to thermal refining treatment (namely, the thermal refining corn leaves are powdery).|[0076] The rest steps are completely consistent.|[0077] Example 5|[0078] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0079] and (3) low-temperature carbon fixation: putting 10g of the tempered corn leaves into a tube furnace for pre-oxidation treatment to obtain pre-oxidized corn leaves; wherein the pre-oxidation treatment temperature is 100 ℃, the pre-oxidation treatment time (namely, the heat preservation time at the pre-oxidation temperature) is 10h, and the heating rate in the process of heating the modified corn leaves to the pre-oxidation temperature is 0.1 ℃/min.|[0080] The rest steps are completely consistent.|[0081] Example 6|[0082] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0083] and (3) low-temperature carbon fixation: putting 10g of the tempered corn leaves into a tube furnace for pre-oxidation treatment to obtain pre-oxidized corn leaves; wherein the pre-oxidation treatment temperature is 350 ℃, the pre-oxidation treatment time (namely, the heat preservation time at the pre-oxidation temperature) is 0.5h, and the heating rate in the process of heating the modified corn leaves to the pre-oxidation temperature is 15 ℃/min.|[0084] The rest steps are completely consistent.|[0085] Example 7|[0086] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0087] a carbonization step: carrying out high-temperature carbonization on the preoxidized corn leaves in a tubular furnace under the nitrogen atmosphere to obtain carbonized corn leaves; wherein the carbonization temperature is 400 ℃, and the carbonization treatment time (the heat preservation time at the carbonization temperature) is 10h; the heating rate in the process of heating the modified corn leaves to the carbonization temperature is 1 ℃/min.|[0088] The rest steps are completely consistent.|[0089] Example 8|[0090] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0091] a carbonization step: carrying out high-temperature carbonization on the preoxidized corn leaves in a tubular furnace under the nitrogen atmosphere to obtain carbonized corn leaves; wherein the carbonization temperature is 1000 ℃, and the carbonization treatment time (the heat preservation time at the carbonization temperature) is 1h; the heating rate of the modified corn leaves in the process of heating to the carbonization temperature is 18 ℃/min.|[0092] The rest steps are completely consistent.|[0093] Example 9|[0094] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0095] the activation temperature in the activation step is 600 ℃, and the time of the activation treatment is 3h.|[0096] The rest steps are completely consistent.|[0097] Example 10|[0098] In the embodiment, the capacitance carbon is prepared by using straw as a biomass raw material, and the specific preparation steps are completely the same as those in the embodiment 1 except that the raw materials are different.|[0099] Example 11|[0100] In the embodiment, the capacitance carbon is prepared by using rice hulls as the biomass raw materials, and the specific preparation steps are completely the same as those in the embodiment 1 except that the raw materials are different.|[0101] Comparative example 1|[0102] Comparative example 1 a capacitance carbon was prepared by the following specific steps:|[0103] carbonizing: cleaning and drying the biomass raw material corn leaves; and then, putting the corn leaves into a tube furnace, and carrying out high-temperature carbonization in a nitrogen atmosphere, wherein the carbonization temperature is 600 ℃, the carbonization time (namely, the heat preservation time at the carbonization temperature) is 4h, and the temperature rise rate is 2 ℃/min, so as to obtain the carbonized corn leaves.|[0104] An activation step: soaking the carbonized corn leaves and KOH in deionized water for 12 hours according to the mass ratio of 1:4; drying the soaked corn leaves, then putting the corn leaves into a tube furnace, and activating the corn leaves in a nitrogen atmosphere; wherein the activation temperature is 800 ℃, and the activation time (namely, the heat preservation time at the activation temperature) is 1h; the heating rate of the soaked corn leaves in the process of heating to the activation temperature is 2 ℃/min. And after the activation is finished, cooling, taking out, washing with acid and water to be neutral, and drying to obtain the capacitance carbon.|[0105] Table 1 is a summary of the properties of the capacitive carbons prepared in examples 1-11 of the present invention.|[0106] TABLE 1|[0107] |[0108] Wherein, table 2 shows the yield data of the capacitance carbon prepared in the inventive example and the comparative example 1.|[0109] TABLE 2|[0110] Capacity charcoal yield (%)Comparative example 117.2Example 125.6Example 229.1Example 328.2Example 427.9Example 535.5Example 637.4Example 740Example 836.3Example 931.7Example 1028.2Example 1130.6|[0111] Wherein, table 3 shows the particle size comparison of the capacitance carbon prepared in the inventive example and comparative example 1.|[0112] TABLE 3|[0113] D10/μmD50/μmD90/μmComparative example 15.69415.28643.850Example 12.1456.41715.366Example 22.3355.82317.651Example 32.6537.84615.237Example 42.0596.85518.112Example 52.5056.36416.830Example 62.2677.14217.287Example 72.4826.81818.059Example 82.2276.95217.854Example 92.5867.58318.302Example 103.0045.99715.339Example 112.7416.02817.295|[0114] Wherein, table 4 shows the comparison of the contents of metal elements in the capacitor carbons prepared in the examples of the present invention and comparative example 1.|[0115] TABLE 4|[0116] |[0117] Wherein, table 5 shows the comparison of CHONS element content in the capacitance carbon prepared by the embodiment of the invention and the comparative example 1.|[0118] TABLE 5|[0119] CHNSOComparative example 189.271.070.260.101.796Example 195..370.960.200.001.814Example 296.020.820.210.001.020Example 395.891.580.190.001.332Example 495.911.320.200.001.565Example 594.671.190.180.001.245Example 695.321.030.200.001.801Example 794.880.850.190.001.367Example 895.331.620.250.001.462Example 996.270.980.320.001.774Example 1094.261.140.110.001.558Example 1195.151.270.260.001.349|[0120] Wherein, table 6 shows the specific capacitance ratios (inorganic system) in the preparation of the capacitance carbon of the examples of the present invention and comparative example 1.|[0121] TABLE 6|[0122] Inorganic system specific capacitance/(F/g)Comparative example 154.9Example 166.3Example 268.1Example 367.3Example 466.2Example 567.5Example 665.2Example 769.3Example 867.7Example 968.6Example 1067.9Example 1167.0|[0123] Wherein, table 7 shows comparison of cycle stability (10000 cycles) in the preparation of the capacitor carbon according to the example of the present invention and the comparative example 1.|[0124] TABLE 7|[0125] Specific capacity retention (%)Comparative example 194.7Example 198.6Example 298.9Example 398.5Example 499.3Example 598.7Example 699.0Example 798.9Example 899.2Example 999.1Example 1099.4Example 1198.8|[0126] As is evident from the data of the above examples, comparative example 1 and tables 1-7: the preparation method of the capacitance carbon provided by the embodiment of the invention can improve the yield, purity and performance of the capacitance carbon.|[0127] The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and any simple modification, equivalent change and modification made to the above embodiment according to the technical spirit of the present invention are still within the scope of the technical solution of the present invention. (CN113511654)|TECHNICAL FIELD|[0001] The invention relates to the technical field of capacitance carbon, in particular to capacitance carbon and a preparation method thereof.|BACKGROUND ART|[0002] The super capacitor has the characteristics of high power, long service life, wide use temperature and the like, and has wide application prospect in the fields of electric vehicles, smart grids, portable electronic equipment and the like.|[0003] The porous carbon material has the characteristics of good conductivity, large specific surface area, stable physicochemical property, rich pore structure and the like, and becomes the electrode material of the super capacitor which is widely researched at present. The commercial super capacitor has very strict requirements on various indexes of the carbon-based electrode material, including ultrahigh purity, large specific surface area, porous structure, high conductivity, high compaction density, low cost and the like, and more than 90% of the carbon material depends on import at present. How to prepare the low-cost and high-performance capacitance carbon material becomes the difficult problem of 'neck' puzzling the development of the super capacitor industry in China.|[0004] At present, the method for preparing capacitance carbon by biomass is to directly carry out carbonization and activation treatment on biomass raw materials to prepare the capacitance carbon. However, the inventor of the invention finds that the existing method has the technical problems of more investment, less output, low yield and poor performance, and cannot meet the requirement of commercialized capacitance carbon.|DISCLOSURE|Disclosure of Invention|[0005] In view of this, the present invention provides a capacitance carbon and a preparation method thereof, and mainly aims to improve the performance, purity and yield of a capacitance carbon material.|[0006] In order to achieve the purpose, the invention mainly provides the following technical scheme:|[0007] in one aspect, an embodiment of the present invention provides a method for preparing capacitance carbon, including the following steps:|[0008] pretreating a source to temper: carrying out pretreatment and thermal refining on the biomass raw material to obtain a thermal-refined biomass raw material; wherein the pretreatment quenching and tempering treatment comprises the steps of crushing, screening, acid washing, water washing and drying the biomass raw material;|[0009] and (3) low-temperature carbon fixation: carrying out pre-oxidation treatment on the biomass raw material after the quenching and tempering treatment to obtain a pre-oxidation product;|[0010] a carbonization step: carbonizing the pre-oxidized product to obtain a carbonized product;|[0011] an activation step: and carrying out activation treatment on the carbonized product to obtain the capacitance carbon.|[0012] Preferably, in the step of the acid washing treatment: the adopted acid solution comprises one or more of hydrochloric acid, nitric acid and sulfuric acid; preferably, the concentration of the acid solution is 0.1-5mol/L; preferably, the step of acid washing treatment specifically comprises: soaking a biomass raw material in the acid solution; preferably, the soaking time is 0.1-24h.|[0013] Preferably, before the step of conditioning the pretreatment source, the method further comprises: and cleaning and drying the biomass raw material.|[0014] Preferably, in the step of conditioning the pretreatment source: the biomass raw material after being crushed is sieved by a sieve with 40 to 200 meshes.|[0015] Preferably, in the step of conditioning the pretreatment source: and washing the biomass raw material subjected to acid washing with deionized water until the biomass raw material is neutral.|[0016] Preferably, in the step of conditioning the pretreatment source: and drying the washed biomass raw material at the temperature of 60-90 ℃ for 2-15h.|[0017] In the low-temperature carbon fixation step: heating the biomass raw material subjected to thermal refining treatment to a pre-oxidation treatment temperature in an air or oxygen atmosphere, and performing pre-oxidation treatment; preferably, the pre-oxidation treatment temperature is 100-350 ℃, and the pre-oxidation treatment time is 0.5-10h; preferably, in the process of heating the biomass raw material after the thermal refining to the pre-oxidation treatment temperature: the heating rate is 0.1-20 deg.C/min.|[0018] In the carbonization step: under the protective atmosphere (nitrogen or argon), heating the pre-oxidized product to a carbonization temperature, carrying out carbonization treatment, and cooling to room temperature to obtain a carbonized product; preferably, the carbonization temperature is 400-1000 ℃, and the carbonization treatment time is 0.5-10h; preferably, during the heating of the pre-oxidation product to the charring temperature: the heating rate is 0.1-20 ℃/min; preferably, after the pre-oxidation treatment in the low-temperature carbon fixation step is finished, the atmosphere is switched to a protective atmosphere, and the pre-oxidation product is heated from the pre-oxidation treatment temperature to the carbonization temperature.|[0019] Preferably, in the activation step: soaking the carbonized product and an activating agent in deionized water according to a set mass ratio for soaking treatment; drying the product after the dipping treatment; and then, heating the product of the dipping treatment to an activation temperature for activation treatment under a protective atmosphere, cooling to room temperature, and washing with water to be neutral to obtain the capacitance carbon. Preferably, the activation temperature is 300-1000 ℃, and the activation treatment time is 0.5-10h; preferably, during heating of the product of the impregnation treatment to the activation temperature: the heating rate is 0.1-20 ℃/min; preferably, the activating agent is KOH, naOH or K 2 CO 3 、Na 2 CO 3 、ZnCl 2 、AlCl 3 And H 3 PO 4 One or more of the above; preferably, in the step of the impregnation treatment: the set mass ratio is 1: (0.1-100). Preferably, the time of the dipping treatment is 0.5 to 24 hours.|[0020] Preferably, the biomass raw material is any one of corn leaves, straws, rice hulls and fruit shells.|[0021] Preferably, the yield of the capacitance carbon prepared by the preparation method of the capacitance carbon is 25-40%.|[0022] In another aspect, an embodiment of the present invention provides a capacitor carbon; wherein the first discharge specific capacitance of the organic system of the capacitance carbon is more than or equal to 35.0F/g; the first discharge specific capacitance of the inorganic system of the capacitance carbon is more than or equal to 65.0F/g; preferably, the cycling stability (the specific capacity retention rate of the capacitance carbon) of the capacitance carbon is more than or equal to 98 percent;|[0023] preferably, the content of metallic elements, namely iron element, in the capacitance carbon is not more than 50mg/kg, the content of nickel element is not more than 50mg/kg, the content of cobalt element is not more than 20mg/kg, the content of copper element is not more than 20mg/kg, the content of sodium element is not more than 100mg/kg, the content of potassium element is not more than 200mg/kg, and the content of aluminum element is not more than 200mg/kg;|[0024] preferably, the capacitance carbon is prepared by the preparation method of any one of the above methods.|[0025] Compared with the prior art, the capacitance carbon and the preparation method thereof have the following beneficial effects:|[0026] the preparation method of the capacitance carbon provided by the embodiment of the invention adopts the treatment technologies of crushing, sieving, acid washing, water washing to neutrality and drying to carry out pretreatment source conditioning on the biomass raw material, solves the problems of high water content, more impurities, irregular particle size and shape distribution, low stacking density, low equipment utilization rate, poor product stability and the like of the biomass raw material, improves the process consistency of the raw material, and is coupled with the subsequent low-temperature carbon fixation-carbonization-activation process technology to prepare the capacitance carbon material with high yield, reasonable particle size distribution, high purity and high specific capacitance. The invention adds a preoxidation process to stabilize the carbon skeleton to prevent carbon elements from being CO and CO 2 The escape of carbon-containing gas micromolecules and the reduction of the generation of liquid products reduce the loss of carbon elements, the yield of solid carbon is improved by 5-20 percent compared with the traditional process, the production cost is reduced, and meanwhile, the addition of the pre-oxidation process does not cause the result of overhigh oxygen content of the product; therefore, thisThe low-temperature carbon fixation technology has important significance for the large-scale production of the biomass-based capacitance carbon material.|[0027] In conclusion, the preparation method of the capacitance carbon provided by the invention adds a pretreatment source quenching and tempering technology and a low-temperature carbon fixing technology before carbonization, so that the purity of the capacitance carbon material is improved, the performance of the capacitance carbon material is optimized, and meanwhile, the yield of the capacitance carbon is greatly improved.|[0028] The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical solutions of the present invention more clearly understood and to make the technical solutions of the present invention practical in accordance with the contents of the specification, the following detailed description is given of preferred embodiments of the present invention with reference to the accompanying drawings.|DRAWINGS DESCRIPTION|[0029] Fig. 1 is a process flow chart of a method for preparing capacitance carbon provided in example 1 of the present invention.|INVENTION MODE|Detailed Description|[0030] To further explain the technical means and effects of the present invention adopted to achieve the predetermined object, the following detailed description of the embodiments, structures, features and effects according to the present invention will be made with reference to the accompanying drawings and preferred embodiments. In the following description, different "one embodiment" or "an embodiment" refers to not necessarily the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.|[0031] On one hand, the embodiment of the invention provides a preparation method of capacitance carbon, which mainly comprises the following process flows: and (3) carrying out pretreatment source conditioning, low-temperature carbon fixation, carbonization and activation processes on the biomass raw material in sequence to obtain the biomass-based capacitance carbon. The method comprises the following specific steps:|[0032] 1) A cleaning step: and cleaning and drying the biomass raw material.|[0033] 2) Pretreating a source to temper: the biomass raw material is subjected to pretreatment and thermal refining, and the pretreatment and thermal refining specifically comprises crushing, sieving, acid washing, deionized water washing to neutrality and drying treatment.|[0034] The acid solution used in the acid washing treatment is one of hydrochloric acid, nitric acid and sulfuric acid, or the acid solution is a mixed solution of a plurality of acids of hydrochloric acid, nitric acid and sulfuric acid. Preferably, the concentration of the acid solution is 0.1-5mol/L; wherein, the time length of soaking the screened biomass raw material in the acid solution is 0.1-24h.|[0035] Wherein the biomass raw material after being crushed is sieved by a sieve of 40-200 meshes. Here, it is required to pass a 40-200 mesh sieve. The selection of the particle size of the raw material is directly related to the subsequent acid washing, pre-oxidation, carbonization and activation processes, and comprises the determination of the conditions of acid concentration, heating temperature, heat preservation time, heating rate, dipping time and the like. Too small a particle size may result in a reduced char yield. Too large a particle size can result in too large a particle size of the final capacitive carbon product, resulting in a decrease in electrochemical performance.|[0036] And drying the washed biomass raw material at the temperature of 60-90 ℃ for 2-15h.|[0037] 3) And (3) low-temperature carbon fixation: performing low-temperature pre-oxidation treatment on the biomass raw material subjected to the quality treatment in a tubular furnace in the air or oxygen atmosphere; wherein the pre-oxidation treatment temperature is 100-350 ℃, the heating rate is 0.1-20 ℃/min, and the pre-oxidation treatment time is 0.5-10h.|[0038] 4) A carbonization step: and (3) switching the reaction atmosphere to nitrogen or argon, continuously heating to 400-1000 ℃ for carbonization treatment at the heating rate of 0.1-20 ℃/min for 0.5-10h, and then cooling to room temperature to obtain a carbonized product.|[0039] 5) An activation step: and (2) soaking the carbonized product and an activating agent in deionized water according to a preset mass ratio, drying after soaking treatment (preferably, the soaking treatment time is 0.5-24h; the use amount of the deionized water does not exceed the use amount of the carbonized product, so that the carbonized product is uniformly soaked in an activating agent aqueous solution), and then performing activating treatment under a protective atmosphere. The protective atmosphere is nitrogen or argon, the activation temperature is 300-1000 ℃, the heating rate is 0.1-20 ℃/min, and the activation treatment time is 0.5-10h. And then cooling to room temperature, and washing with deionized water to be neutral to obtain the capacitance carbon.|[0040] Wherein the activating agent is KOH, naOH or K 2 CO 3 、Na 2 CO 3 、ZnCl 2 、AlCl 3 And H 3 PO 4 Or the activating agent is KOH, naOH or K 2 CO 3 、Na 2 CO 3 、ZnCl 2 、AlCl 3 And H 3 PO 4 A mixture of a plurality of (a). The preset mass ratio of the carbonized product to the activating agent is 1:0.1-100.|[0041] In the prior art, the method for preparing the capacitance carbon by using the biomass raw material is to directly carbonize and activate the biomass raw material to prepare the capacitance carbon. Compared with the prior art, the preparation process of the capacitive carbon provided by the invention adds two technologies of pretreatment source tempering and low-temperature carbon fixation before the carbonization step, namely the biomass-based capacitive carbon is prepared by adopting a pretreatment source tempering-low Wen Gutan-carbonization-activation process. Compared with the prior art, the process provided by the invention has the advantages that the performance of the capacitance carbon material is optimized, the purity is improved and the yield of the capacitance carbon is greatly improved after the pretreatment source quenching and tempering process and the low-temperature carbon fixation process are additionally arranged. The specific analysis is as follows:|[0042] first, a pretreatment source conditioning technology|[0043] Compared with the traditional fossil fuel, the biomass raw material has the disadvantages of low bulk density and energy density, high water content, strong hygroscopicity (hydrophilicity), difficult grinding, poor liquidity and the like; these disadvantages pose challenges and problems to the biomass thermochemical conversion and treatment process:|[0044] (1) The low bulk density is detrimental to the storage and transportation of the biomass feedstock, resulting in increased costs for storage and transportation of the biomass feedstock. The low energy density limits the overall capacity scale of the biomass thermodynamic system, reducing the economics of the biomass energy source. High water content in the biomass raw material can delay pyrolysis reaction, influence the yield of pyrolysis products and the stability of the products, and increase the heat supply cost. In addition, the defects of high water content, irregular particle size and shape distribution, low bulk density and the like of the biomass raw material cause poor fluidity of the biomass raw material, and further cause the failure of a biomass raw material feeding system, which is a main factor for limiting the further amplification of the industrial utilization scale of the biomass. On the other hand, due to the difference of biomass raw material types and production places, wherein the relative components of hemicellulose, cellulose, lignin and ash are greatly changed, the biomass pyrolysis characteristics and the product distribution are greatly influenced.|[0045] Therefore, the pretreatment source conditioning technology can be used for improving certain physical and chemical properties of the biomass raw materials and is coupled with the subsequent pyrolysis technology, the purpose of maximizing the utilization value of pyrolysis products is achieved, and meanwhile, the difference among different biomass raw materials is reduced due to the use of the technology, so that the technology disclosed by the invention has universal applicability.|[0046] (2) The particle size and the morphology of the raw materials influence the dynamic parameter change (drying, heating rate and reaction rate) of biomass particles and the particle size and the morphology of the final product capacitance carbon material; the particle size distribution and the particle size of the capacitance carbon material influence the specific surface area and the tap density, so that the processing technology and the rate capability of the electrode material are influenced.|[0047] (3) The activated carbon is used as a key electrode material, and the purity of the activated carbon directly determines the performance of the supercapacitor. The metal ions (iron, nickel, cobalt, copper, sodium, potassium, aluminum, etc.) in the activated carbon undergo redox reactions during charging to generate leakage current, thereby causing the voltage of the capacitor to drop. At the same time, the ions also affect the cycling stability of the capacitor, resulting in a reduced lifetime. Therefore, the removal of impurity metal ions and the improvement of the purity of the activated carbon have important significance for improving the performance of the capacitor.|[0048] Aiming at the problems of the biomass raw material, the invention adopts the treatment technologies of crushing, sieving, acid washing, water washing to neutrality and drying to carry out pretreatment source conditioning on the biomass raw material, solves the problems of high water content, more impurities, irregular particle size and shape distribution, low stacking density, low equipment utilization rate, poor product stability and the like of the raw material, improves the process consistency of the raw material, and is coupled with the subsequent low-temperature carbon fixation-carbonization-activation process technology to prepare the capacitance carbon material with high yield, reasonable particle size distribution, high purity and high specific capacitance.|[0049] Here, repeated emphasis is given to: the biomass raw material has the following problems: (1) High water content in the biomass raw material can delay pyrolysis reaction, influence the yield and product stability of pyrolysis products, and increase heat supply cost, so that the raw material is dried; (2) The size and shape distribution of the raw material particles can influence mass transfer and heat transfer of the subsequent process, so that the raw material is crushed and sieved; (3) The relative composition of hemicellulose, cellulose, lignin and ash in the raw material is greatly changed due to the difference of biomass types and production places, the biomass pyrolysis characteristics and the product distribution are greatly influenced, the raw material is purified through acid treatment, the difference among different biomass raw materials is reduced, and the subsequent process has universal applicability. Based on this, through long-term and large-scale experimental research, the particle sizes with different meshes are matched with corresponding processes of low-temperature carbon fixation, carbonization, activation and the like, and the final physical and chemical properties of the target product of the invention can be obtained. "move the whole body by pulling one movement", there is a relationship of correlation and coupling between each process parameter.|[0050] Second, low temperature carbon sequestration|[0051] In the prior art, the problems of more investment, less output and low yield exist in the process of preparing the carbon material by using the biomass. The advantages of low equipment productivity and low raw material cost can be reduced, and the commercialization requirement of the capacitance carbon can not be met. Therefore, the improvement of the carbon yield becomes a core problem of the industrial production of the biomass carbon material.|[0052] The pyrolysis of the biomass raw material can generate gas, liquid and solid three-state products, and carbon elements can be CO and CO 2 And the carbon-containing gas micromolecules, liquid products such as acids, phenols, ketones, alcohols, esters and the like and solid carbon are distributed, and the yield of the three products has a competitive relationship. Based on the method, the low-temperature carbon fixation technology is added to the existing manufacturing process, and the carbon skeleton is stabilized through pre-oxidation to prevent carbon elements from being CO and CO 2 And the escape of carbon-containing gas micromolecules and the reduction of the generation of liquid products reduce the loss of carbon elements, improve the yield of solid carbon by 5-20 percent compared with the traditional process and reduce the production cost. In addition, oxygen-containing functional groups on the surface of the capacitance carbon have strong electrochemical activity and are easy to generate decomposition reaction during charging and discharging, so that the cycle stability of the super capacitor is reduced. At the same time, the oxygen-containing functional groups reduce the materialThe equivalent series internal resistance is increased, and the power density and the cycle life of the capacitor are reduced. Therefore, the method has great scientific significance and application value in controlling the oxygen content of the capacitance carbon material. In the invention, the addition of the low-temperature carbon fixation technology has no consequence of over-high oxygen content of the product. Therefore, the low-temperature carbon fixation technology has important significance for the large-scale production of the biomass-based capacitance carbon material.|[0053] The invention is further illustrated by the following specific experimental examples:|[0054] example 1|[0055] In this example, a capacitance carbon is prepared, as shown in fig. 1, by the following main preparation steps:|[0056] 1) Cleaning and drying the biomass raw material corn leaves.|[0057] 2) Pretreating a source to temper:|[0058] crushing the corn leaves treated in the step 1), sieving the crushed corn leaves with a 60-mesh sieve, then soaking the crushed corn leaves in a proper amount of 1mol/L hydrochloric acid solution, washing the crushed corn leaves with deionized water to be neutral after 12 hours, and drying the washed corn leaves (the drying temperature is 60 ℃ and the drying time is 15 hours) to obtain the corn leaves (namely, the modified corn leaves are powdery) after the modification treatment.|[0059] 3) Low temperature carbon fixation step|[0060] Putting 10g of the tempered corn leaves into a tube furnace for pre-oxidation treatment to obtain pre-oxidized corn leaves; wherein the pre-oxidation treatment temperature is 200 ℃, the pre-oxidation treatment time (namely, the heat preservation time at the pre-oxidation treatment temperature) is 2h, and the heating rate in the process of heating the modified corn leaves to the pre-oxidation treatment temperature is 2 ℃/min.|[0061] 4) Carbonization step|[0062] Carbonizing the pre-oxidized corn leaves in a tubular furnace in nitrogen atmosphere to obtain carbonized corn leaves; wherein the carbonization temperature is 600 ℃, and the carbonization treatment time (the heat preservation time at the carbonization temperature) is 4h; the heating rate in the process of heating the modified corn leaves to the carbonization temperature is 2 ℃/min.|[0063] 5) Step of activation|[0064] Soaking the carbonized corn leaves and KOH in deionized water according to the mass ratio of 1:4 for 12 hours; drying the corn leaves after the dipping treatment, then putting the corn leaves into a tube furnace, and carrying out activation treatment in a nitrogen atmosphere; wherein the activation temperature is 800 ℃, the activation treatment time is 1h, and the temperature rise rate in the process of heating the corn leaves after the dipping treatment to the activation temperature is 2 ℃/min. And after the activation is finished, cooling, taking out, washing with acid and water to be neutral, and drying to obtain the capacitance carbon.|[0065] Example 2|[0066] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0067] in the activation step of this embodiment, the selected activating agent is sodium carbonate, and the carbonized corn leaves and the sodium carbonate are mixed according to a mass ratio of 1:10, and immersing in deionized water for 20 hours.|[0068] The rest steps are completely consistent.|[0069] Example 3|[0070] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0071] pretreating a source to temper: crushing the corn leaves treated in the step 1), sieving the crushed corn leaves with a 60-mesh sieve, then soaking the crushed corn leaves in a proper amount of 0.1mol/L sulfuric acid solution, washing the crushed corn leaves with deionized water to be neutral after 24 hours, and drying the washed corn leaves to obtain the corn leaves subjected to thermal refining (namely, the thermal refining corn leaves are powdery).|[0072] The rest steps are completely consistent.|[0073] Example 4|[0074] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0075] pretreating a source to temper: crushing the corn leaves treated in the step 1), sieving the crushed corn leaves with a 60-mesh sieve, then soaking the crushed corn leaves in a proper amount of 5mol/L hydrochloric acid solution, washing the crushed corn leaves with deionized water to be neutral after 0.1 hour, and drying the washed corn leaves to obtain the corn leaves subjected to thermal refining treatment (namely, the thermal refining corn leaves are powdery).|[0076] The rest steps are completely consistent.|[0077] Example 5|[0078] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0079] and (3) low-temperature carbon fixation: putting 10g of the tempered corn leaves into a tube furnace for pre-oxidation treatment to obtain pre-oxidized corn leaves; wherein the pre-oxidation treatment temperature is 100 ℃, the pre-oxidation treatment time (namely, the heat preservation time at the pre-oxidation temperature) is 10h, and the heating rate in the process of heating the modified corn leaves to the pre-oxidation temperature is 0.1 ℃/min.|[0080] The rest steps are completely consistent.|[0081] Example 6|[0082] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0083] and (3) low-temperature carbon fixation: putting 10g of the tempered corn leaves into a tube furnace for pre-oxidation treatment to obtain pre-oxidized corn leaves; wherein the pre-oxidation treatment temperature is 350 ℃, the pre-oxidation treatment time (namely, the heat preservation time at the pre-oxidation temperature) is 0.5h, and the heating rate in the process of heating the modified corn leaves to the pre-oxidation temperature is 15 ℃/min.|[0084] The rest steps are completely consistent.|[0085] Example 7|[0086] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0087] a carbonization step: carrying out high-temperature carbonization on the preoxidized corn leaves in a tubular furnace under the nitrogen atmosphere to obtain carbonized corn leaves; wherein the carbonization temperature is 400 ℃, and the carbonization treatment time (the heat preservation time at the carbonization temperature) is 10h; the heating rate in the process of heating the modified corn leaves to the carbonization temperature is 1 ℃/min.|[0088] The rest steps are completely consistent.|[0089] Example 8|[0090] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0091] a carbonization step: carrying out high-temperature carbonization on the preoxidized corn leaves in a tubular furnace under the nitrogen atmosphere to obtain carbonized corn leaves; wherein the carbonization temperature is 1000 ℃, and the carbonization treatment time (the heat preservation time at the carbonization temperature) is 1h; the heating rate of the modified corn leaves in the process of heating to the carbonization temperature is 18 ℃/min.|[0092] The rest steps are completely consistent.|[0093] Example 9|[0094] In the embodiment, the biomass raw material corn leaves are adopted to prepare the capacitance carbon; this example differs from the preparation procedure of example 1 in that:|[0095] the activation temperature in the activation step is 600 ℃, and the time of the activation treatment is 3h.|[0096] The rest steps are completely consistent.|[0097] Example 10|[0098] In the embodiment, the capacitance carbon is prepared by using straw as a biomass raw material, and the specific preparation steps are completely the same as those in the embodiment 1 except that the raw materials are different.|[0099] Example 11|[0100] In the embodiment, the capacitance carbon is prepared by using rice hulls as the biomass raw materials, and the specific preparation steps are completely the same as those in the embodiment 1 except that the raw materials are different.|[0101] Comparative example 1|[0102] Comparative example 1 a capacitance carbon was prepared by the following specific steps:|[0103] carbonizing: cleaning and drying the biomass raw material corn leaves; and then, putting the corn leaves into a tube furnace, and carrying out high-temperature carbonization in a nitrogen atmosphere, wherein the carbonization temperature is 600 ℃, the carbonization time (namely, the heat preservation time at the carbonization temperature) is 4h, and the temperature rise rate is 2 ℃/min, so as to obtain the carbonized corn leaves.|[0104] An activation step: soaking the carbonized corn leaves and KOH in deionized water for 12 hours according to the mass ratio of 1:4; drying the soaked corn leaves, then putting the corn leaves into a tube furnace, and activating the corn leaves in a nitrogen atmosphere; wherein the activation temperature is 800 ℃, and the activation time (namely, the heat preservation time at the activation temperature) is 1h; the heating rate of the soaked corn leaves in the process of heating to the activation temperature is 2 ℃/min. And after the activation is finished, cooling, taking out, washing with acid and water to be neutral, and drying to obtain the capacitance carbon.|[0105] Table 1 is a summary of the properties of the capacitive carbons prepared in examples 1-11 of the present invention.|[0106] TABLE 1|[0107] |[0108] Wherein, table 2 shows the yield data of the capacitance carbon prepared in the inventive example and the comparative example 1.|[0109] TABLE 2|[0110] Capacity charcoal yield (%)Comparative example 117.2Example 125.6Example 229.1Example 328.2Example 427.9Example 535.5Example 637.4Example 740Example 836.3Example 931.7Example 1028.2Example 1130.6|[0111] Wherein, table 3 shows the particle size comparison of the capacitance carbon prepared in the inventive example and comparative example 1.|[0112] TABLE 3|[0113] D10/μmD50/μmD90/μmComparative example 15.69415.28643.850Example 12.1456.41715.366Example 22.3355.82317.651Example 32.6537.84615.237Example 42.0596.85518.112Example 52.5056.36416.830Example 62.2677.14217.287Example 72.4826.81818.059Example 82.2276.95217.854Example 92.5867.58318.302Example 103.0045.99715.339Example 112.7416.02817.295|[0114] Wherein, table 4 shows the comparison of the contents of metal elements in the capacitor carbons prepared in the examples of the present invention and comparative example 1.|[0115] TABLE 4|[0116] |[0117] Wherein, table 5 shows the comparison of CHONS element content in the capacitance carbon prepared by the embodiment of the invention and the comparative example 1.|[0118] TABLE 5|[0119] CHNSOComparative example 189.271.070.260.101.796Example 195..370.960.200.001.814Example 296.020.820.210.001.020Example 395.891.580.190.001.332Example 495.911.320.200.001.565Example 594.671.190.180.001.245Example 695.321.030.200.001.801Example 794.880.850.190.001.367Example 895.331.620.250.001.462Example 996.270.980.320.001.774Example 1094.261.140.110.001.558Example 1195.151.270.260.001.349|[0120] Wherein, table 6 shows the specific capacitance ratios (inorganic system) in the preparation of the capacitance carbon of the examples of the present invention and comparative example 1.|[0121] TABLE 6|[0122] Inorganic system specific capacitance/(F/g)Comparative example 154.9Example 166.3Example 268.1Example 367.3Example 466.2Example 567.5Example 665.2Example 769.3Example 867.7Example 968.6Example 1067.9Example 1167.0|[0123] Wherein, table 7 shows comparison of cycle stability (10000 cycles) in the preparation of the capacitor carbon according to the example of the present invention and the comparative example 1.|[0124] TABLE 7|[0125] Specific capacity retention (%)Comparative example 194.7Example 198.6Example 298.9Example 398.5Example 499.3Example 598.7Example 699.0Example 798.9Example 899.2Example 999.1Example 1099.4Example 1198.8|[0126] As is evident from the data of the above examples, comparative example 1 and tables 1-7: the preparation method of the capacitance carbon provided by the embodiment of the invention can improve the yield, purity and performance of the capacitance carbon.|[0127] The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and any simple modification, equivalent change and modification made to the above embodiment according to the technical spirit of the present invention are still within the scope of the technical solution of the present invention. Family Number|(96539972)|96539972|Abstract|(CN113511654B B)|The invention relates to capacitor carbon and a preparation method thereof , and relates to the technical field of capacitor carbon . According to the main technical scheme , the preparation method of the capacitance carbon comprises the following steps : a pretreatment source tempering step : carrying out pretreatment tempering treatment on a biomass raw material to obtain the biomass raw material subjected to tempering treatment ; wherein the pretreatment tempering treatment comprises the steps of conducting crushing , sieving , pickling , water washing and drying on the biomass raw material ; a low - temperature carbon sequestration step : carrying out pre - oxidation treatment on the biomass raw material subjected to thermal refining treatment to obtain a pre - oxidation product ; a carbonization step : carrying out carbonization treatment on the pre - oxidized product to obtain a carbonized product ; and an activation step : performing activation treatment on the carbonized product to obtain the capacitor carbon . According to the method , after the pretreatment source tempering process and the low - temperature carbon sequestration process are added , the purity of the capacitor carbon is improved , the performance is optimized , and meanwhile , the yield of the capacitor carbon is also greatly improved . |CPC codes|(CN113511654B B)|C01B - 032/324 |C01B - 032/342 |C01B - 032/348 |IPC codes|(CN113511654B B)|C01B - 032/324 |C01B - 032/342 |C01B - 032/348 | Electrical machinery, apparatus, energy|Materials, metallurgy C01B-032/324|C01B-032/342|C01B-032/348|H01G-011/34|H01G-011/44|Y02E-060/13 C01B-032/324|C01B-032/342|C01B-032/348|H01G-011/34|H01G-011/44|Y02E-060/13 C01B-032/324|C01B-032/342|C01B-032/348|H01G-011/34|H01G-011/44 C01B-032/324|C01B-032/342|C01B-032/348|H01G-011/34|H01G-011/44 CN117049536|CN116924396|CN118711996B|CN116947038B CN117049536 107275424 WHO=Examiner SELF=N CAT=A|CN116924396 106980900 WHO=Examiner SELF=Y CAT=A|CN118711996B 111615099 WHO=Examiner SELF=N|CN116947038B 107012952 WHO=Examiner SELF=N CN111547723|CN108439402|CN112225194|CN110817867|CN110240161|CN109835900|CN108455595|CN106946250|CN106117610|CN105540582|CN106904613|CN102153081|US5776384|CN110723734|CN105036108|CN1837039 CN111547723 90258898 WHO=Examiner SELF=N CAT=Y|CN108439402 81031451 WHO=Examiner SELF=N CAT=Y|CN112225194 92338154 WHO=Examiner SELF=N CAT=A|CN110817867 87734622 WHO=Examiner SELF=N CAT=A|CN110240161 86027006 WHO=Examiner SELF=N CAT=A|CN109835900 84728700 WHO=Examiner SELF=N CAT=A|CN108455595 81034977 WHO=Examiner SELF=N CAT=A|CN106946250 76778560 WHO=Examiner SELF=N CAT=A|CN106117610 74607485 WHO=Examiner SELF=N CAT=A|CN105540582 72847521 WHO=Examiner SELF=N CAT=A|CN106904613 76647644 WHO=Examiner SELF=N CAT=A|CN102153081 7345734 WHO=Examiner SELF=N CAT=A|US5776384 43009774 WHO=Examiner SELF=N CAT=A|CN110723734 87430946 WHO=Examiner SELF=N|CN105036108 71315108 WHO=Examiner SELF=N|CN1837039 5297552 WHO=Examiner SELF=N 辛凡文等: &quot;高比表面活性炭的研究进展及应用现状&quot;, 《2015年中国化工学会年会论文集》 (Cat. Y)|陈志敏: &quot;生物质基分级多孔炭的制备及电化学性能研究&quot;, 《中国博士学位论文全文数据库 工程科技Ⅰ辑》 (Cat. A) US5776384; CN102153081; CN105540582; CN106946250; CN108439402; CN108455595; CN109835900; CN110240161; CN110817867; CN111547723; CN112225194; CN106117610; CN106904613; CN110723734; CN1837039; CN105036108 GRANTED (CN113511654)|GRANTED ALIVE (CN113511654)|ALIVE (CN113511654)|LEGAL DETAILS FOR CN113511654|Actual or expected expiration date=2041-04-16|Legal state=ALIVE|Status=GRANTED|Event publication date=2021-04-16|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202110411481|Application date=2021-04-16|Standardized application number=2021CN-0411481|Event publication date=2021-10-19|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN113511654|Publication stage code=A|Publication date=2021-10-19|Standardized publication number=CN113511654|Event publication date=2021-10-19|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2021-11-05|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2022-11-15|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN113511654|Publication stage code=B|Publication date=2022-11-15|Standardized publication number=CN113511654B|Event publication date=2022-11-15|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN113511654)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRqPCnIYuh8Ixj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000065405503&ekey=1949&xpn=CN113511654B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=fB%252BjR%252BMfaavWfDGX1p4lpbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN113511654)|CN|(CN113511654)|CN (CN113511654)|NAME=SHANXI INSTITUTE OF COAL CHEMISTRY CHINESE ACADEMY OF SCIENCES , COUNTRY=CN|(CN113511654)|NAME=SHANXI INSTITUTE OF COAL CHEMISTRY CHINESE ACADEMY OF SCIENCES , COUNTRY=CN (CN113511654)|NAME=LIANG YONGFANG;BEIJING XURUN LAW FIRM , REG=11522|(CN113511654)|NAME=LIANG YONGFANG;BEIJING XURUN LAW FIRM , REG=11522 (CN113511654)|NAME=YUAN SHUXIA|NAME=ZHOU JINGJIE|(CN113511654)|NAME=YUAN SHUXIA|NAME=ZHOU JINGJIE 0 1 Titre: (CN113511654)|Capacitance carbon and preparation method thereof Résumé: (CN113511654)|The invention relates to capacitor carbon and a preparation method thereof, and relates to the technical field of capacitor carbon. According to the main technical scheme, the preparation method of the capacitance carbon comprises the following steps: a pretreatment source tempering step: carrying out pretreatment tempering treatment on a biomass raw material to obtain the biomass raw material subjected to tempering treatment; wherein the pretreatment tempering treatment comprises the steps of conducting crushing, sieving, pickling, water washing and drying on the biomass raw material; a low-temperature carbon sequestration step: carrying out pre-oxidation treatment on the biomass raw material subjected to thermal refining treatment to obtain a pre-oxidation product; a carbonization step: carrying out carbonization treatment on the pre-oxidized product to obtain a carbonized product; and an activation step: performing activation treatment on the carbonized product to obtain the capacitor carbon. According to the method, after the pretreatment source tempering process and the low-temperature carbon sequestration process are added, the purity of the capacitor carbon is improved, the performance is optimized, and meanwhile, the yield of the capacitor carbon is also greatly improved. 75 Abstract gpt-4o-mini no The article focuses on the preparation of capacitor carbon and its related processes, which do not involve accelerated weathering or CO₂ capture through mineral alteration.
76 IN202441017388 IN202441017388 IN202441017388 116031041 IN202441017388 A 2025-09-12 [IN202441017388] 2024-03-11 2024-03-11 2025-09-12 (IN202441017388)|2044-03-11 (IN202441017388)|System and method for preparing carbonate-enhanced nutrition composition using geo-bags (IN202441017388)|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand. HYPERWORKS IMAGING PRIVATE (IN202441017388)|HYPERWORKS IMAGING PRIVATE LIMITED Tannirkulam Ajay|Margankunte Naveen (IN202441017388)|Tannirkulam Ajay|Margankunte Naveen (IN202441017388)|1. A method for preparing a carbonate-enhanced nutrition composition using a geo-bag (112) wherein the method comprising: i) Collecting and crushing rocks into small particles, using a rock crushing unit (102); ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbon-sequestration substrate, using a reactor (108) by Characterized in that, a) mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions; and b) filling the carbon-sequestration substrate into the geo-bag (112) to prepare carbon-sequestration packages, wherein the geo-bag (112) comprises an ecofriendly material that permits only water and air to pass through while retaining the substrate inside, wherein the geo-bag (112) comprises a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbonsequestration substrate by subjecting the carbon-sequestration packages to a rockcarbonation period at an operating location to capture atmospheric carbon dioxide; wherein the geo-bag (112) acts as a structural member providing a high surface area-tovolume ratio to optimize carbon dioxide capture resulting 15 to 130 times enhanced carbonation efficiency.| (IN202441017388)|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112.|Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.| (IN202441017388)|GEOBAG(100,42)|CARBONATE ENHANCED NUTRITION(100,29)|ROCK CRUSHING(57,8)|CARBONSEQUESTRATION SUBSTRATE(48,2)|CARBON SEQUESTRATION SUBSTRATE(44,31)|ENHANCED CARBONATION(44,3)|URBAN ORGANIC WASTAGE COLLECTION(41,4)|CARBON SEQUESTRATION(37,42)|ROCK CARBONATION PERIOD(35,9)|MIX CRUSHED ROCK(33,1)|CARBON DIOXIDE CAPTURE(32,1)|GRAVEL(31,21)|BIOMASS(28,12)|CARBON SEQUESTRATION PACKAGE(26,8)|SUBSTRATE INSIDE(26,1)|MIXING CONDITION(24,6)|FERTILIZER(24,4)|ATMOSPHERIC CARBON DIOXIDE(24,2)|ECOFRIENDLY MATERIAL(24,1)|REACTOR(23,14)|OUTDOOR ENVIRONMENT(23,4)|BAG CONTENT(20,3)|ORGANIC ACID EXTRACTION(19,8)|ACETIC ACID COMPOUND(18,2)|POTASH(17,6)|GEOTEXTILE(17,4)|MOISTURE CONTENT(17,4)|AGRICULTURE(16,2)|CARBON DIOXIDE(15,17)|CALCIUM CARBONATE(15,6)|DECOMPOSITION(15,3)|MICROALGAE(15,3)|CO2 LEVEL(15,2)|OLIVINE(14,3)|VOLUME RATIO(14,2)|ACETIC ACID(13,8)|ROCK CRUSHER(13,3)|STONE WEIGHT(11,4)|PH VALUE RANGING(11,3)|ACCELERATE WEATHERING(11,2)|CELLULOSE DERIVED MONOSACCHARIDE(11,2)|CONCENTRATION LEVEL RANGING(11,2)|HDPE(11,2)|MAGNESIUM CARBONATE(11,2)|SMALL PARTICLE(10,6)|TRANSPORTATION MEDIUM(10,5)|ECO FRIENDLY MATERIAL(10,4)|BUILDING CONSTRUCTION(10,1)|CARBONATED ENHANCED NUTRITION(10,1)|THANTHE NATURAL CARBONATION(10,1)|TOA CARBON MINERALIZATION(10,1)|MIXING TEMPERATURE(9,4)|SUPERCRITICAL CONDITION(9,4)|DUNITE ANALYSIS(9,3)|ELECTRO MICROBIAL PRODUCTION(9,2)|REFILL CARTRIDGE(9,2)|ROCK CARBONATION PERIOD RANGE(9,2)|BASALT IC ROCK(9,1)|LIQUEFIED BIOMASS CONVERSION(9,1)|ORGANIC ACID COMPONENT(8,18)|CONDITION OPTIMIZATION(8,6)|EXPERIMENTAL SETUP(8,2)|LIQUEFACTION REACTION(8,2)|ACCELERATE CARBONATION(8,1)|BIOMASS LIQUEFACTION(8,1)|CONE CRUSHING(8,1)|MINERAL DISSOLUTION REACTOR(8,1)|STONE SIZE(7,12)|CARBONIZATION(7,11)|HEAVY METAL(7,6)|CARBONATION MENSTRUATION(7,3)|FURFURAL ACID LACTIC(7,3)|STRUCTURAL MEMBER(7,3)|VALUED MATERIAL(6,8)|PPM(6,4)|DIKETO GLUCONIC ACID(6,2)|NONOPTIMIZED CONDITION(6,2)|SAND SPRAY(6,2)|BURIED FORA(6,1)|CARBONATION REACTOR(6,1)|CRUSHED ROCK RETRIEVAL(6,1)|FARMING LAND(6,1)|FEEDER BREAKER(6,1)|MITIGATE ISSUE(6,1)|NUTRITION ENHANCEMENT(6,1)|RAW BASALT SAMPLE(6,1)|RAW DUNITE SAMPLE(6,1)|ATMOSPHERIC PRESSURE(5,4)|CONSTRUCTION SITE(5,3)|TRAPPING(5,3)|BALL MILL CRUSHER(5,1)|BASALT ANALYSIS(5,1)|CARBONATION PERFORMANCE(5,1)|DIKETOGLUCONIC ACID(5,1)|DUNITEROCK SAMPLE(5,1)|FEEDING ROCK(5,1)|OPTIMIZED CARBONATION CONDITION(5,1)|URBAN ORGANIC WASTE COLLECTION(5,1)|FILLING STATION(4,4)|GRAPHICAL REPRESENTATION(4,4)|WEIGHT VOLUME(4,4)|FIBER DENSITY(4,2)|SOLID MINERAL(4,2)|SYSTEM COMPLICATION(4,2)|ASTHE REACTED CARBON REMAINS(4,1)|BIO CATALYST COMBINATION(4,1)|CARBON DIOXIDE SEQUESTRATION(4,1)|CARBONATE ENHANCED MINERAL FORMATION(4,1)|CARBONSEQUESTRATION(4,1)|CO MINERALIZATION(4,1)|DISPENSATION(4,1)|EXCAVATOR(4,1)|GYRATORY CRUSHER(4,1)|OPTIMIZED ENVIRONMENT(4,1)|PRIMARY COMPARTMENT(4,1)|SIGNIFICANTRISEINATMOSPHERIC CARBON DIOXIDE(4,1)|SYSTEMFORPREPARING(4,1)| (IN202441017388)|1. A method for preparing a carbonate-enhanced nutrition composition using a geo-bag (112) wherein the method comprising: i) Collecting and crushing rocks into small particles, using a rock crushing unit (102); ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbon-sequestration substrate, using a reactor (108) by Characterized in that, a) mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions; and b) filling the carbon-sequestration substrate into the geo-bag (112) to prepare carbon-sequestration packages, wherein the geo-bag (112) comprises an ecofriendly material that permits only water and air to pass through while retaining the substrate inside, wherein the geo-bag (112) comprises a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbonsequestration substrate by subjecting the carbon-sequestration packages to a rockcarbonation period at an operating location to capture atmospheric carbon dioxide; wherein the geo-bag (112) acts as a structural member providing a high surface area-tovolume ratio to optimize carbon dioxide capture resulting 15 to 130 times enhanced carbonation efficiency.|2. The method as claimed in claim 1, wherein the crushed rocks comprise at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof, wherein the crushed rocks comprises of a particle size below 5 mm.|3. The method as claimed in claim 1, wherein the predefined mixing conditions comprise a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2 atm.|4. The method as claimed in claim 1, wherein the carbon-sequestration substrate comprises a concentration level ranging from 400 part per million (ppm) to 450 ppm, a moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.|5. The method as claimed in claim 1, wherein the geo-bag (112) comprises at least one of geotextiles, high-density polyethylene (HDPE), and/or a combination thereof.|6. The method as claimed in claim 1, wherein the rock-carbonation period ranges from 2 years to 5 years.|7. The method as claimed in claim 1, wherein the organic acid component is extracted using an electro-microbial production (EMP) technique from the biomass; wherein the biomass is generated from the decomposition of at least one of organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.|8. The method as claimed in claim 1, wherein the operating location comprises at least one of farming land, a construction site, an outdoor environment.|9. The method as claimed in claim 1, wherein the method comprises extracting high-value materials from the carbonate-enhanced composition, wherein the high-value materials comprise at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals and/or a combination thereof.|10. The method as claimed in claim 1, wherein the carbonate-enhanced composition is used as fertilizer in agriculture and/or as M-sand in the construction field. (IN202441017388)|Technical Field|[0001] The embodiments herein generally relate toa carbon mineralization method, and more particularly, a system and method for preparing carbonate-enhanced nutrition composition using a geo-bag. Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.|Description of the Related Art|[0002] In recent years, the significantriseinatmospheric carbon dioxide (CO2) levels has been identified as a leading cause of climate change on Earth. To mitigate this issue, carbon mineralization, or carbon sequestration, has emerged as a prominent method. Carbon mineralization is a process of converting carbon dioxide into solid minerals, such as carbonate, through a chemical reaction. This reaction occurs when specific types of rocks, such as serpentine, basalt, mafic, ultramafic, etc., are exposed to carbon dioxide, resulting in the formation of carbonate-enhanced minerals. Hence, the atmospheric CO2 level is stabilized asthe reacted carbon remains bound within the solid minerals, preventing its release into the atmosphere. However, it is important to note that this process typically requires several years to effectively reduce carbon levels in the atmosphere.|[0003] Most of the existing carbon sequestration systemsto produce carbonate-enhanced mineralsutilize indoor techniques, employingan indirect method. For example, thesesystemsincludea mineral dissolution reactor for mixing various materials. These materials include magnesium or calcium, which is available in the rocks (e.g. serpentine, olivine, basalt, or labradorite), organic acid, and chelating agents. Through this mixing process, a magnesium or calcium-rich solvent is synthesized tocapture and store carbon dioxide. Additionally, these existing systemsinclude a combined biocatalyst and carbonation reactor, along witha control module for expediting the process of sequestration of carbon. However, the current indoor technique requires a more complicated arrangement and entails higher costs.|[0004] Accordingly, there remains a need for a more simple and direct approach to capture and store the carbon dioxide from the atmosphere at a reduced economic level and to produce a carbonated enhanced nutrition composition using a geo-bag.|SUMMARY|[0005] In view of a foregoing, an embodiment herein provides a method for preparing a carbonate-enhanced nutrition composition using a geo-bag. The method includes i) collecting and crushing rocks into small particles, using a rock crushing unit; ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbonsequestration substrate using a reactor by mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions. The carbon-sequestration substrate is filled into geo-bags to prepare carbon-sequestration packages. The geo-bag includes an eco-friendly material that only permits water and air to pass through while retaining the substrate. The geo-bag consists of a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbon-sequestration substrate by subjecting the carbonsequestration packages to a rock-carbonation period at an operating location to capture atmospheric carbon dioxide. The geo-bag acts as a structural member providing a high surface area-to-volume ratio to optimize carbon dioxide capture resulting in 15 to 130 times enhanced carbonation efficiency.|[0006] In some embodiments, the crushed rocks include at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof. The crushed rocks include a particle size below 5 mm.|[0007] In some embodiments, the predefined mixing conditions include a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2|atm.|[0008] In some embodiments, the carbon-sequestration substrate includes a concentration level ranging from 400 parts per million (ppm) to 450 ppm, a moisture content ranging from|25% to 95% of rock weight and a pH value ranging from 2.5 to 3.5.|[0009] In some embodiments, the geo-bag includes at least one of the geotextiles, highdensity polyethylene (HDPE), and/or a combination thereof.|[0010] In some embodiments, the rock-carbonation period ranges from 2 years to 5 years.|[0011] In some embodiments, the organic acid component is extracted using an electromicrobial production (EMP) technique from the biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.|[0012] In some embodiments, the operating location includes at least one farming land, a construction site, and an outdoor environment.|[0013] In some embodiments, the method includes extracting high-value materials from the carbonate-enhanced nutrition composition, wherein the high-value materials include at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals, and/or a combination thereof.|[0014] In some embodiments, the carbonate-enhanced nutrition composition is used as fertilizer in agriculture and/or as M-sand in the construction field.|[0015] . In some embodiments, the refill docking platform includes a connection part that is configured to hold the refill cartridge in an invertedly upright position to enable the flow of the substance from the refill cartridge to the bottom of the primary compartment.|[0016] The method of preparing a carbonate-enhanced nutrition composition of the present description includes a more direct approach for capturing and storing carbon dioxide from the atmosphere using the geo-bag. The direct approach represents the geo-bag that includes a simple configuration used in an outdoor environment for capturing and storing carbon dioxide from the atmosphere. Such a simple configuration of geo-bag eliminates the need for a complicated arrangement of the carbon dioxide sequestration system used in the existing system.|The geo-bag includes improved measurement, reporting, and verification (MRV) by enclosing the first mixture in a high surface area to volume ratio and staking in vertical layers to hold the first mixture, and the geo-bag acts as a structural member to produce a carbonate enhanced nutrition composition at a lower economical level. Such carbonate-enhanced nutrition composition includes high economic value materials, which can be used as a fertilizer for agricultural fields or building construction material, e.g. M-sand.|[0017] These and other aspects of the embodiments herein will be better appreciated and understood when considered in conjunction with the following description and the accompanying drawings. It should be understood, however, that the following descriptions, while indicating preferred embodiments and numerous specific details thereof, are given by way of illustration and not of limitation. Many changes and modifications may be made within the scope of the embodiments herein without departing from the spirit thereof, and the embodiments herein include all such modifications.|BRIEF DESCRIPTION OF THE DRAWINGS|[0018] The embodiments herein will be better understood from the following detailed description with reference to the drawings, in which:|[0019] FIG. 1 is a block diagram that illustrates a systemforpreparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein;|[0020] FIG. 2 illustrates a process of preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein;|[0021] FIGS. 3A- 3Bareflow diagrams that illustratea method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein; and|[0022] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS. 3A-3B of the present disclosure according to some embodiments herein.|DETAILED|DESCRIPTION OF PREFERRED EMBODIMENTS|[0023] The embodiments herein and the various features and advantageous details thereof are explained more fully with reference to the non-limiting embodiments that are illustrated in the accompanying drawings and detailed in the following description. Descriptions of well-known components and processing techniques are omitted so as to not unnecessarily obscure the embodiments herein. The examples used herein are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the examples should not be construed as limiting the scope of the embodiments herein.|[0024] In the view of the foregoing, the need for a system and methodfor producing carbonate-enhanced nutrition composition using a geo-bag is in the ongoing description.|Referring now to the drawings, and more particularly to FIGS. 1 through 4D, where similar reference characters denote corresponding features in a consistent manner throughout the figures, there are shown preferred embodiments.|[0025] FIG. 1 is a block diagram that illustrates a system 100for preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. The system 100 includesa rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The rock crushing unit 102 receives rocks from a source station for compressing and breaking the rocks into small particles. In some embodiments, the source station may be a quarry or a mining area, and the rock is extracted using explosives or mechanical excavators to remove the rock from the ground. The rock crushing unit 102 may include an input unit, a series of crushing and screening units, a transporting unit, and a storage area. The input unit may include a hopper for feeding the rocks and is passed through the series of crushing and screening units for compressing and breaking the rocks into desiredsizes to obtain crushed rocks. The crushed rocks are forwarded to the transporting unit. The transporting unit may include a conveyor belt that carries the crushed rocks to the storage area or an end location. In some embodiments, the crushing and screening unit includes but is not limited to a jaw crusher, a cone crusher, an impact crusher, a gyratory crusher, a ball mill crusher, a feeder breaker, a roll crusher, or a combination thereof.|[0026] The reactor 108 is connected to the rock crushing unit 102 for receiving the smaller particles of crushed rocks. The urban organic wastage collection unit 104 receives municipal waste and is connected to the organic acid extraction unit 106 to produce organic acidcomponents through an electro-microbial process (EMP). The urban organic wastage collection unit 104 collects and stores organic waste, including municipal solid waste, industrial organic wastes, and or agricultural wastes to produce a biomass material. The biomass material may be produced using a microbial technique.|[0027] The reactor 108 is connected to the organic acid extraction unit 106 to mix the organic acid componentthat is extracted from a biomass materialwith the crushed rocks to prepare a carbon-sequestration substrate. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere. In some embodiments, the organic acid component is extracted by a liquefaction reaction of biomass under supercritical conditions. The liquefaction reaction of biomass under supercritical conditions results in an effective decomposition of biomass. The supercritical condition may include the addition of water to the biomass and increasing its temperature above the boiling point of the water at which the water has a high pressure and high concentration of H+ and OH- ions. Such supercritical conditions help the conversion of liquefied biomass into cellulose-derived monosaccharides. The cellulosederived monosaccharide is degraded into some short-chain intermediates in the absence of oxidant to produce value-added chemicals that includethe organic acid components. The organic acid components may include but are not limited to acetic acid, citric acid, 2,5-diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid or 2,5-furandicarboxylic acid (FDCA).|[0028] The reactor 108 is configured for mixing about 70% to 90% of weight/weight|(w/w) of the crushed rocks and about 10% to 30% weight/volume (w/V) of the organic acid components to prepare a carbon-sequestration substrate at a predetermined mixing condition.|The predetermined mixing condition may include a mixing temperature ranging from 25°C to|30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over 2 hours - 48 hours to prepare thecarbon-sequestration substrate.|[0029] The geo-bag 112 receives the carbon-sequestration substrate from the reactor 108|through a spray head. The carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.|[0030] The conveyor unit 110 is configured for carrying the carbon-sequestration substrate to a filling station from the reactor 108. The filling station is provided with the geo-bag|112. In some embodiments, the geo-bag 112 is made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 112. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE),or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3 millimeters (mm). The geo-bag 112 is made from eco-friendly materials that do not decompose over the rock carbonation period, allow selective exchange of material between the bag contents and the environment, and allow retrieval of crushed rock post the carbonation period.|[0031] The geo-bag 112 is filled with the carbon-sequestration substrate to prepare a carbon-sequestration package. In some embodiments, the geo-bag 112 is filled by dispensing the carbon-sequestration substratethrough a sand spray head that is arranged in the reactor 108. The dispensation of the carbon-sequestration substrateis controlled from the reactor 108 in the thickness of 1 cm to 12 inches at rates of 40-200 tons/hr.|[0032] The carbon-sequestration packages are transferred to an operating location using a transportation medium. The transportation medium may be a conveyor belt, truck, or manual process.|[0033] The carbon-sequestration packages are allowed for a rock carbonation period in the operating location by stacking or burying the packages in the operating location. The rock carbonation period may be 2-5 years. The carbon-sequestration substratein a package is enabled to capture the carbon dioxide from the atmosphere and convert thecarbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Thereby, the concentration level of|CO2 in the atmosphere is reduced. The carbonate-enhanced nutrition compositionincludes high economic value materials, including but not limited to calcium carbonate, potash, phosphate, and heavy metals.|[0034] FIG. 2 illustrates a process 200 for preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein. The process 200 includes a stone crusher 202, a sand grinding ball mill 204, a conveyor unit 206, and a geo-bag 208. The stone crusher 202includes a series of cone crushing units and an automatic feeding arrangement for receiving rock from a source station (e.g.mining area or quarry)for compressing and breaking the rocks into small particles to obtain crushed rocks. The sand grinding ball mill 204 receives the crushed rocks from thestone crusher 202 and mixes the crushed rocks with an organic acid component at a predetermined mixing condition to prepare a carbon-sequestration substrate. The organic acid component is extracted from biomass using an organic acid extraction unit. The conveyor unit 206 carries the carbon-sequestration substrateto a filling station from the sand grinding ball mill 204. The filling station is provided withthe geo-bag 208, whichis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 208. The geo-bag 208 is filled with the carbon-sequestration substrateto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportationmedium. The packages are stacked or buried fora rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere resulting in the conversion of the carbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Such carbonate-enhanced nutrition composition includes high economic value materials including but not limited to calcium carbonate, potash, phosphate, and heavy metals.|[0035] FIGS. 3A-3B are flow diagrams that illustrate a method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. At step|302, the method includes receiving the rocks from the ground and preparing the crushed rocks by compressing and breaking the rocks into small particles using the rock crushing unit. The crushed rocks include a particle size below 5 mm.|[0036] At step 304, the method includes collecting and storing organic wastes using the urban organic waste collection unit to produce biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof. The biomass material may be produced using a microbial technique.|[0037] At step 306, the method includes extracting an organic acid component from the biomass using the organic acid extraction unit. The organic acid component may be extracted using an electro-microbial production (EMP) technique. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketogluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-|Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere.|[0038] At step 308, the method includes mixing the crushed rocks in a concentration ranging from 70% to 90% of weight/weight (w/w) and the organic acid component in a concentration ranging from 10% to 30% weight/volume (w/V) to prepare a carbon-sequestration substrate at a predetermined mixing condition using the reactor. The predetermined mixing condition may include a mixing temperature ranging from 25°C to 30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over a few hours to a few days of the period to prepare the carbon-sequestration substrate. In some embodiments, the carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and pH value ranging from 2.5 to 3.5.|[0039] At step 310, the method includes preparing the geo-bagusing an eco-friendly material that allows selective exchange of material between the bag contents and the environment. The geo-bag does not decompose over the rock carbonation period and allows retrieval of a carbonate-enhanced nutrition composition during the carbonation period. The geo20|bagis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE), or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3|millimeters (mm).|[0040] At step 312, the method includes filling the carbon-sequestration substrate, using a sand spray head arranged in the reactor, into the geo-bagto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportation medium.|The transportation medium may be a conveyor belt, a truck, or a manual process.|[0041] At step 314, the method includes allowing the carbon-sequestration packages at a rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere. The packages are stacked or buried in the operating location at the rock carbonation period to capture the carbon dioxide from the atmosphere, resulting in the conversion of the carbon-sequestration substrate into a carbonate-enhanced nutrition composition, thereby reducing environmental CO2 level in the atmosphere. The rock carbonation period may include|2-5 years. In some embodiments, the operating location is a forming land, construction site, or any other outdoor environment. The carbonate-enhanced nutrition composition is further processed to extract high economic value materials, including but are not limited to calcium carbonate, potash, phosphate, and heavy metals.|[0042] TABLE 1 illustrates an approximate concentration level of high-value materials present in the carbonate-enhanced nutrition composition prepared using the method as described in FIG. 3 of the proposed disclosure.|[0043] TABLE 1:|Material Concentration level in percentage|Potassium (K2O) 0.2 %|Phosphate (P2O5) 0.4%|Chromium 0.7%|Nickel 0.7%|CaCO3 4%|[0044] TABLE 2 illustrates experimental results validating the efficiency of the carbonate-enhanced nutrition composition prepared using the method described in FIG. 3 of the present disclosure. The experiments are conducted to accelerate carbonation within a controlled environment, optimizing specific parameters to enhance carbon sequestration efficiency. The study evaluates carbonation performance under varying pH levels and particle sizes to identify the most effective conditions for CO₂ mineralization.|[0045] TABLE 2:|Samples|Carbonization efficiency (%)|Experiment A|pH - 2.5 to 3.5|Rock Size - < 5 mm|Experiment B|pH - 6.0 to 6.5|rock - < 300 microns|Dunite 60.77 22.7|Basalt 14.33 7.5|[0046] The above tabulation shows the experimental setup includes two different conditions: Experiment A is conducted at a pH range of 2.5 to 3.5 with crushed rock samples of less than 5 mm, while Experiment B is conducted at a pH range of 6.0 to 6.5 with a finer particle size of less than 300 microns. The process is carried out within a temperature range of 25°C to|30°C, in a background bath of acetic acid, ensuring an optimized environment for carbonation.|[0047] The results demonstrated significant differences in carbonation efficiency between the two experimental setups. Dunite samples exhibited a carbonation efficiency of|60.77% in Experiment A (pH 2.5 to 3.5, rock size <5 mm), and the efficiency dropped to 22.7%|in Experiment B (pH 6.0 to 6.5, rock size<300 microns). Similarly, basalt samples showed a carbonation efficiency of 14.33% in Experiment A, which reduced to 7.5% in Experiment B. The experimental results demonstrate that lower pH values and larger particle sizes enhanced carbonation particularly at the optimized conditions including pH 2.5 to 3.5 and the rock size is|<5 mm.|[0048] The experiment resultsdemonstrate that the carbonation efficiency is increased 15|to 130 times higher thanthe natural carbonation process with the optimized conditions, including pH value ranging from 2.5 to 3.5 and the rock Size, includes less than 5 mm. These results validate the technical feasibility and efficiency gains of the method described in FIG. 3 of the proposed disclosure, confirming that the integration of crushed ultramafic and basaltic rocks, organic acid-based substrates, and a controlled carbonation process significantly enhances CO₂|capture and mineralization efficiency.|[0049] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3Bof the present disclosure according to some embodiments herein. The analysis shows the elemental compositions of dunite and basalt samples before and after carbonization process. FIGS. 4A - 4B are graphical representations illustrating the X-ray fluorescence (XRF) analysis of dunite rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the duniterock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw dunite rock samples; (iv) A - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out at the optimized condition including pH 2.5 to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5|and the rock size including <300 microns. The results indicate that dunite samples subjected to carbonization under optimized conditions (pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw dunite samples and those carbonized under non-optimized conditions (pH 6.0-6.5, rock size <300 microns).|[0050] FIGS. 4C - 4D are graphical representations illustrating the X-ray fluorescence|(XRF) analysis of basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the basalt rock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw basalt rock samples; (iv) A - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out at the optimized condition including pH 2.5|to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5 and the rock size including <300 microns.|The results indicate that basalt samples subjected to carbonization under optimized conditions|(pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw basalt samples and those carbonized under non-optimized conditions (pH 6.0-|6.5, rock size <300 microns). The higher retention and conversion efficiency of valuable elements under optimized carbonation conditions confirm that the process facilitates effective mineralization and enhances sequestration efficiency.|[0051] The foregoing description of the specific embodiments will so fully reveal the general nature of the embodiments herein that others can, by applying current knowledge, readily modify and/or adapt for various applications such specific embodiments without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments.|It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. Therefore, while the embodiments herein have been described in terms of preferred embodiments, those skilled in the art will recognize that the embodiments herein can be practiced with modification within the spirit and scope. (IN202441017388)|Technical Field|[0001] The embodiments herein generally relate toa carbon mineralization method, and more particularly, a system and method for preparing carbonate-enhanced nutrition composition using a geo-bag. Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.|Description of the Related Art|[0002] In recent years, the significantriseinatmospheric carbon dioxide (CO2) levels has been identified as a leading cause of climate change on Earth. To mitigate this issue, carbon mineralization, or carbon sequestration, has emerged as a prominent method. Carbon mineralization is a process of converting carbon dioxide into solid minerals, such as carbonate, through a chemical reaction. This reaction occurs when specific types of rocks, such as serpentine, basalt, mafic, ultramafic, etc., are exposed to carbon dioxide, resulting in the formation of carbonate-enhanced minerals. Hence, the atmospheric CO2 level is stabilized asthe reacted carbon remains bound within the solid minerals, preventing its release into the atmosphere. However, it is important to note that this process typically requires several years to effectively reduce carbon levels in the atmosphere.|[0003] Most of the existing carbon sequestration systemsto produce carbonate-enhanced mineralsutilize indoor techniques, employingan indirect method. For example, thesesystemsincludea mineral dissolution reactor for mixing various materials. These materials include magnesium or calcium, which is available in the rocks (e.g. serpentine, olivine, basalt, or labradorite), organic acid, and chelating agents. Through this mixing process, a magnesium or calcium-rich solvent is synthesized tocapture and store carbon dioxide. Additionally, these existing systemsinclude a combined biocatalyst and carbonation reactor, along witha control module for expediting the process of sequestration of carbon. However, the current indoor technique requires a more complicated arrangement and entails higher costs.|[0004] Accordingly, there remains a need for a more simple and direct approach to capture and store the carbon dioxide from the atmosphere at a reduced economic level and to produce a carbonated enhanced nutrition composition using a geo-bag.|SUMMARY|[0005] In view of a foregoing, an embodiment herein provides a method for preparing a carbonate-enhanced nutrition composition using a geo-bag. The method includes i) collecting and crushing rocks into small particles, using a rock crushing unit; ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbonsequestration substrate using a reactor by mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions. The carbon-sequestration substrate is filled into geo-bags to prepare carbon-sequestration packages. The geo-bag includes an eco-friendly material that only permits water and air to pass through while retaining the substrate. The geo-bag consists of a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbon-sequestration substrate by subjecting the carbonsequestration packages to a rock-carbonation period at an operating location to capture atmospheric carbon dioxide. The geo-bag acts as a structural member providing a high surface area-to-volume ratio to optimize carbon dioxide capture resulting in 15 to 130 times enhanced carbonation efficiency.|[0006] In some embodiments, the crushed rocks include at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof. The crushed rocks include a particle size below 5 mm.|[0007] In some embodiments, the predefined mixing conditions include a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2|atm.|[0008] In some embodiments, the carbon-sequestration substrate includes a concentration level ranging from 400 parts per million (ppm) to 450 ppm, a moisture content ranging from|25% to 95% of rock weight and a pH value ranging from 2.5 to 3.5.|[0009] In some embodiments, the geo-bag includes at least one of the geotextiles, highdensity polyethylene (HDPE), and/or a combination thereof.|[0010] In some embodiments, the rock-carbonation period ranges from 2 years to 5 years.|[0011] In some embodiments, the organic acid component is extracted using an electromicrobial production (EMP) technique from the biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.|[0012] In some embodiments, the operating location includes at least one farming land, a construction site, and an outdoor environment.|[0013] In some embodiments, the method includes extracting high-value materials from the carbonate-enhanced nutrition composition, wherein the high-value materials include at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals, and/or a combination thereof.|[0014] In some embodiments, the carbonate-enhanced nutrition composition is used as fertilizer in agriculture and/or as M-sand in the construction field.|[0015] . In some embodiments, the refill docking platform includes a connection part that is configured to hold the refill cartridge in an invertedly upright position to enable the flow of the substance from the refill cartridge to the bottom of the primary compartment.|[0016] The method of preparing a carbonate-enhanced nutrition composition of the present description includes a more direct approach for capturing and storing carbon dioxide from the atmosphere using the geo-bag. The direct approach represents the geo-bag that includes a simple configuration used in an outdoor environment for capturing and storing carbon dioxide from the atmosphere. Such a simple configuration of geo-bag eliminates the need for a complicated arrangement of the carbon dioxide sequestration system used in the existing system.|The geo-bag includes improved measurement, reporting, and verification (MRV) by enclosing the first mixture in a high surface area to volume ratio and staking in vertical layers to hold the first mixture, and the geo-bag acts as a structural member to produce a carbonate enhanced nutrition composition at a lower economical level. Such carbonate-enhanced nutrition composition includes high economic value materials, which can be used as a fertilizer for agricultural fields or building construction material, e.g. M-sand.|[0017] These and other aspects of the embodiments herein will be better appreciated and understood when considered in conjunction with the following description and the accompanying drawings. It should be understood, however, that the following descriptions, while indicating preferred embodiments and numerous specific details thereof, are given by way of illustration and not of limitation. Many changes and modifications may be made within the scope of the embodiments herein without departing from the spirit thereof, and the embodiments herein include all such modifications.|BRIEF DESCRIPTION OF THE DRAWINGS|[0018] The embodiments herein will be better understood from the following detailed description with reference to the drawings, in which:|[0019] FIG. 1 is a block diagram that illustrates a systemforpreparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein;|[0020] FIG. 2 illustrates a process of preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein;|[0021] FIGS. 3A- 3Bareflow diagrams that illustratea method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein; and|[0022] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS. 3A-3B of the present disclosure according to some embodiments herein.|DETAILED|DESCRIPTION OF PREFERRED EMBODIMENTS|[0023] The embodiments herein and the various features and advantageous details thereof are explained more fully with reference to the non-limiting embodiments that are illustrated in the accompanying drawings and detailed in the following description. Descriptions of well-known components and processing techniques are omitted so as to not unnecessarily obscure the embodiments herein. The examples used herein are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the examples should not be construed as limiting the scope of the embodiments herein.|[0024] In the view of the foregoing, the need for a system and methodfor producing carbonate-enhanced nutrition composition using a geo-bag is in the ongoing description.|Referring now to the drawings, and more particularly to FIGS. 1 through 4D, where similar reference characters denote corresponding features in a consistent manner throughout the figures, there are shown preferred embodiments.|[0025] FIG. 1 is a block diagram that illustrates a system 100for preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. The system 100 includesa rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The rock crushing unit 102 receives rocks from a source station for compressing and breaking the rocks into small particles. In some embodiments, the source station may be a quarry or a mining area, and the rock is extracted using explosives or mechanical excavators to remove the rock from the ground. The rock crushing unit 102 may include an input unit, a series of crushing and screening units, a transporting unit, and a storage area. The input unit may include a hopper for feeding the rocks and is passed through the series of crushing and screening units for compressing and breaking the rocks into desiredsizes to obtain crushed rocks. The crushed rocks are forwarded to the transporting unit. The transporting unit may include a conveyor belt that carries the crushed rocks to the storage area or an end location. In some embodiments, the crushing and screening unit includes but is not limited to a jaw crusher, a cone crusher, an impact crusher, a gyratory crusher, a ball mill crusher, a feeder breaker, a roll crusher, or a combination thereof.|[0026] The reactor 108 is connected to the rock crushing unit 102 for receiving the smaller particles of crushed rocks. The urban organic wastage collection unit 104 receives municipal waste and is connected to the organic acid extraction unit 106 to produce organic acidcomponents through an electro-microbial process (EMP). The urban organic wastage collection unit 104 collects and stores organic waste, including municipal solid waste, industrial organic wastes, and or agricultural wastes to produce a biomass material. The biomass material may be produced using a microbial technique.|[0027] The reactor 108 is connected to the organic acid extraction unit 106 to mix the organic acid componentthat is extracted from a biomass materialwith the crushed rocks to prepare a carbon-sequestration substrate. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere. In some embodiments, the organic acid component is extracted by a liquefaction reaction of biomass under supercritical conditions. The liquefaction reaction of biomass under supercritical conditions results in an effective decomposition of biomass. The supercritical condition may include the addition of water to the biomass and increasing its temperature above the boiling point of the water at which the water has a high pressure and high concentration of H+ and OH- ions. Such supercritical conditions help the conversion of liquefied biomass into cellulose-derived monosaccharides. The cellulosederived monosaccharide is degraded into some short-chain intermediates in the absence of oxidant to produce value-added chemicals that includethe organic acid components. The organic acid components may include but are not limited to acetic acid, citric acid, 2,5-diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid or 2,5-furandicarboxylic acid (FDCA).|[0028] The reactor 108 is configured for mixing about 70% to 90% of weight/weight|(w/w) of the crushed rocks and about 10% to 30% weight/volume (w/V) of the organic acid components to prepare a carbon-sequestration substrate at a predetermined mixing condition.|The predetermined mixing condition may include a mixing temperature ranging from 25°C to|30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over 2 hours - 48 hours to prepare thecarbon-sequestration substrate.|[0029] The geo-bag 112 receives the carbon-sequestration substrate from the reactor 108|through a spray head. The carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.|[0030] The conveyor unit 110 is configured for carrying the carbon-sequestration substrate to a filling station from the reactor 108. The filling station is provided with the geo-bag|112. In some embodiments, the geo-bag 112 is made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 112. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE),or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3 millimeters (mm). The geo-bag 112 is made from eco-friendly materials that do not decompose over the rock carbonation period, allow selective exchange of material between the bag contents and the environment, and allow retrieval of crushed rock post the carbonation period.|[0031] The geo-bag 112 is filled with the carbon-sequestration substrate to prepare a carbon-sequestration package. In some embodiments, the geo-bag 112 is filled by dispensing the carbon-sequestration substratethrough a sand spray head that is arranged in the reactor 108. The dispensation of the carbon-sequestration substrateis controlled from the reactor 108 in the thickness of 1 cm to 12 inches at rates of 40-200 tons/hr.|[0032] The carbon-sequestration packages are transferred to an operating location using a transportation medium. The transportation medium may be a conveyor belt, truck, or manual process.|[0033] The carbon-sequestration packages are allowed for a rock carbonation period in the operating location by stacking or burying the packages in the operating location. The rock carbonation period may be 2-5 years. The carbon-sequestration substratein a package is enabled to capture the carbon dioxide from the atmosphere and convert thecarbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Thereby, the concentration level of|CO2 in the atmosphere is reduced. The carbonate-enhanced nutrition compositionincludes high economic value materials, including but not limited to calcium carbonate, potash, phosphate, and heavy metals.|[0034] FIG. 2 illustrates a process 200 for preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein. The process 200 includes a stone crusher 202, a sand grinding ball mill 204, a conveyor unit 206, and a geo-bag 208. The stone crusher 202includes a series of cone crushing units and an automatic feeding arrangement for receiving rock from a source station (e.g.mining area or quarry)for compressing and breaking the rocks into small particles to obtain crushed rocks. The sand grinding ball mill 204 receives the crushed rocks from thestone crusher 202 and mixes the crushed rocks with an organic acid component at a predetermined mixing condition to prepare a carbon-sequestration substrate. The organic acid component is extracted from biomass using an organic acid extraction unit. The conveyor unit 206 carries the carbon-sequestration substrateto a filling station from the sand grinding ball mill 204. The filling station is provided withthe geo-bag 208, whichis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 208. The geo-bag 208 is filled with the carbon-sequestration substrateto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportationmedium. The packages are stacked or buried fora rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere resulting in the conversion of the carbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Such carbonate-enhanced nutrition composition includes high economic value materials including but not limited to calcium carbonate, potash, phosphate, and heavy metals.|[0035] FIGS. 3A-3B are flow diagrams that illustrate a method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. At step|302, the method includes receiving the rocks from the ground and preparing the crushed rocks by compressing and breaking the rocks into small particles using the rock crushing unit. The crushed rocks include a particle size below 5 mm.|[0036] At step 304, the method includes collecting and storing organic wastes using the urban organic waste collection unit to produce biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof. The biomass material may be produced using a microbial technique.|[0037] At step 306, the method includes extracting an organic acid component from the biomass using the organic acid extraction unit. The organic acid component may be extracted using an electro-microbial production (EMP) technique. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketogluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-|Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere.|[0038] At step 308, the method includes mixing the crushed rocks in a concentration ranging from 70% to 90% of weight/weight (w/w) and the organic acid component in a concentration ranging from 10% to 30% weight/volume (w/V) to prepare a carbon-sequestration substrate at a predetermined mixing condition using the reactor. The predetermined mixing condition may include a mixing temperature ranging from 25°C to 30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over a few hours to a few days of the period to prepare the carbon-sequestration substrate. In some embodiments, the carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and pH value ranging from 2.5 to 3.5.|[0039] At step 310, the method includes preparing the geo-bagusing an eco-friendly material that allows selective exchange of material between the bag contents and the environment. The geo-bag does not decompose over the rock carbonation period and allows retrieval of a carbonate-enhanced nutrition composition during the carbonation period. The geo20|bagis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE), or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3|millimeters (mm).|[0040] At step 312, the method includes filling the carbon-sequestration substrate, using a sand spray head arranged in the reactor, into the geo-bagto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportation medium.|The transportation medium may be a conveyor belt, a truck, or a manual process.|[0041] At step 314, the method includes allowing the carbon-sequestration packages at a rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere. The packages are stacked or buried in the operating location at the rock carbonation period to capture the carbon dioxide from the atmosphere, resulting in the conversion of the carbon-sequestration substrate into a carbonate-enhanced nutrition composition, thereby reducing environmental CO2 level in the atmosphere. The rock carbonation period may include|2-5 years. In some embodiments, the operating location is a forming land, construction site, or any other outdoor environment. The carbonate-enhanced nutrition composition is further processed to extract high economic value materials, including but are not limited to calcium carbonate, potash, phosphate, and heavy metals.|[0042] TABLE 1 illustrates an approximate concentration level of high-value materials present in the carbonate-enhanced nutrition composition prepared using the method as described in FIG. 3 of the proposed disclosure.|[0043] TABLE 1:|Material Concentration level in percentage|Potassium (K2O) 0.2 %|Phosphate (P2O5) 0.4%|Chromium 0.7%|Nickel 0.7%|CaCO3 4%|[0044] TABLE 2 illustrates experimental results validating the efficiency of the carbonate-enhanced nutrition composition prepared using the method described in FIG. 3 of the present disclosure. The experiments are conducted to accelerate carbonation within a controlled environment, optimizing specific parameters to enhance carbon sequestration efficiency. The study evaluates carbonation performance under varying pH levels and particle sizes to identify the most effective conditions for CO₂ mineralization.|[0045] TABLE 2:|Samples|Carbonization efficiency (%)|Experiment A|pH - 2.5 to 3.5|Rock Size - < 5 mm|Experiment B|pH - 6.0 to 6.5|rock - < 300 microns|Dunite 60.77 22.7|Basalt 14.33 7.5|[0046] The above tabulation shows the experimental setup includes two different conditions: Experiment A is conducted at a pH range of 2.5 to 3.5 with crushed rock samples of less than 5 mm, while Experiment B is conducted at a pH range of 6.0 to 6.5 with a finer particle size of less than 300 microns. The process is carried out within a temperature range of 25°C to|30°C, in a background bath of acetic acid, ensuring an optimized environment for carbonation.|[0047] The results demonstrated significant differences in carbonation efficiency between the two experimental setups. Dunite samples exhibited a carbonation efficiency of|60.77% in Experiment A (pH 2.5 to 3.5, rock size <5 mm), and the efficiency dropped to 22.7%|in Experiment B (pH 6.0 to 6.5, rock size<300 microns). Similarly, basalt samples showed a carbonation efficiency of 14.33% in Experiment A, which reduced to 7.5% in Experiment B. The experimental results demonstrate that lower pH values and larger particle sizes enhanced carbonation particularly at the optimized conditions including pH 2.5 to 3.5 and the rock size is|<5 mm.|[0048] The experiment resultsdemonstrate that the carbonation efficiency is increased 15|to 130 times higher thanthe natural carbonation process with the optimized conditions, including pH value ranging from 2.5 to 3.5 and the rock Size, includes less than 5 mm. These results validate the technical feasibility and efficiency gains of the method described in FIG. 3 of the proposed disclosure, confirming that the integration of crushed ultramafic and basaltic rocks, organic acid-based substrates, and a controlled carbonation process significantly enhances CO₂|capture and mineralization efficiency.|[0049] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3Bof the present disclosure according to some embodiments herein. The analysis shows the elemental compositions of dunite and basalt samples before and after carbonization process. FIGS. 4A - 4B are graphical representations illustrating the X-ray fluorescence (XRF) analysis of dunite rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the duniterock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw dunite rock samples; (iv) A - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out at the optimized condition including pH 2.5 to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5|and the rock size including <300 microns. The results indicate that dunite samples subjected to carbonization under optimized conditions (pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw dunite samples and those carbonized under non-optimized conditions (pH 6.0-6.5, rock size <300 microns).|[0050] FIGS. 4C - 4D are graphical representations illustrating the X-ray fluorescence|(XRF) analysis of basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the basalt rock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw basalt rock samples; (iv) A - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out at the optimized condition including pH 2.5|to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5 and the rock size including <300 microns.|The results indicate that basalt samples subjected to carbonization under optimized conditions|(pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw basalt samples and those carbonized under non-optimized conditions (pH 6.0-|6.5, rock size <300 microns). The higher retention and conversion efficiency of valuable elements under optimized carbonation conditions confirm that the process facilitates effective mineralization and enhances sequestration efficiency.|[0051] The foregoing description of the specific embodiments will so fully reveal the general nature of the embodiments herein that others can, by applying current knowledge, readily modify and/or adapt for various applications such specific embodiments without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments.|It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. Therefore, while the embodiments herein have been described in terms of preferred embodiments, those skilled in the art will recognize that the embodiments herein can be practiced with modification within the spirit and scope. Family Number|(116031041)|116031041|Abstract|(IN202441017388 A)|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand.|IPC codes|(IN202441017388 A)|A01G-024/12|A01G-024/15|A01G-024/17|A01G-024/20|A01G-024/60| Other special machines A01G-024/12|A01G-024/15|A01G-024/17|A01G-024/20|A01G-024/60 A01G-024/12|A01G-024/15|A01G-024/17|A01G-024/20|A01G-024/60 PENDING (IN202441017388)|PENDING ALIVE (IN202441017388)|ALIVE (IN202441017388)|LEGAL DETAILS FOR IN202441017388|Actual or expected expiration date=2044-03-11|Legal state=ALIVE|Status=PENDING|Event publication date=2024-03-11|Event code=IN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=IN IN202441017388|Application date=2024-03-11|Standardized application number=2024IN-41017388|Event publication date=2025-09-12|Event code=IN/A|Event indicator=Pos|Event group=Examination events|Application laid open|Publication country=IN|Publication number=IN202441017388|Publication stage code=A|Publication date=2025-09-12|Standardized publication number=IN202441017388 (IN202441017388)|IN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=/WizbbSQlgu/uP20qNF3JE9lJnxGv8IZa/WZFbsCsqzB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=IN0000000001670167&ekey=2476&xpn=IN202441017388&kind=A https://iprsearch.ipindia.gov.in/PublicSearch/PublicationSearch/ApplicationStatus https://permalink.orbit.com/RenderStaticFirstPage?XPN=dR15du4ks0vl9J154pQkJcExnvIz5kLrfqHome9U%252B8A%3D%26n%3D1&id=0&base=FAMPAT IN (IN202441017388)|NAME=Tannirkulam Ajay|NAME=Margankunte Naveen 0 1 Titre: (IN202441017388)|System and method for preparing carbonate-enhanced nutrition composition using geo-bags Résumé: (IN202441017388)|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand. 72 Abstract gpt-4o-mini yes The article describes a system for preparing a carbon-sequestration substrate that captures CO₂ and converts it into carbonates, aligning with the topic of enhanced weathering and carbon sequestration.
77 US63/601,059P|US18/954,208 US18/954,208 US20250164404 114579754 US20250164404 A1 2025-05-22 [US20250164404] 2023-11-20|2024-11-20 2024-11-20 2025-05-22 (US20250164404)|2044-11-20 (US20250164404)|System and method for enhanced rock weathering monitoring, reporting, and verification (US20250164404)|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering. IMPOSSIBLE SENSING|MATI CARBON PBC (US20250164404)|Impossible Sensing LLC ([US])|Mati Carbon PBC ([US]) SOBRON PABLO|JORDAN JACOB S|AGARWAL SHANTANU (US20250164404)|Sobron Pablo|Jordan Jacob S.|Agarwal Shantanu (US20250164404)|By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement.|The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402.|This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status.|However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions.|However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land.|MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved.| (US20250164404)|1. A system for monitoring, reporting, and verification of enhanced rock weathering comprising: a spectroscopy device comprising an optical source and a detector, wherein the optical source is configured to emit one or more optical signals directed to a target collected from a target area, and the detector is configured to determine spectral measurements of the optical signals collected from the target; and a data analysis subsystem coupled to the spectroscopy device and configured to: convert the spectral measurements to data indicating compositional characteristics of the target; analyze the data indicating compositional characteristics of the target using a plurality of analytical tools; and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.|14. A method for monitoring, reporting, and verification of enhanced rock weathering comprising: emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area; determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target; and converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target; analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools; and providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.| (US20250164404)|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW.|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil.|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304.| (US20250164404)|ENHANCED ROCK(100,22)|REPORTING(100,13)|MONITORING(100,11)|VERIFICATION(100,7)|ENHANCED ROCK VERIFICATION(100,4)|SPECTRAL MEASUREMENT(90,13)|SPECTROSCOPY(69,19)|ANALYTICAL INSTRUMENT(59,9)|WEATHERING STATUS(56,9)|DRY LAND EVALUATION(55,1)|ENHANCED ROCK WEATHERING VERIFICATION(51,2)|SOIL COMPLEXITY(51,1)|ASSESSMENT(48,10)|DATA ANALYSIS SUBSYSTEM(47,25)|WEATHERING PREDICTION(45,6)|INSIGHT(41,13)|IDENTIFYING GEOLOCATED ZONE(41,1)|STATISTICAL ACCURACY(40,1)|EMPIRICAL MODEL(38,7)|MULTIVARIATE DISTRIBUTION MODEL(36,6)|VALUABLE INSIGHT(36,3)|POOLED SAMPLE(33,12)|ECOSYSTEMATIC CHANGE(32,1)|HEAVY CATION(29,2)|CATION COVARIANCE ANALYSIS(28,6)|ROCK LOSS(27,3)|SIGNAL TRANSMITTER(26,2)|LONG TIMESCALE(26,1)|EARTH AUGER(25,5)|CARBON CREDIT CREATION(24,6)|ENHANCED WEATHERING POTENTIAL(23,7)|CARBON DIOXIDE REMOVAL(22,31)|LAND SINGLE PLOT(22,1)|UNCERTAINTY(21,2)|DATA ANALYSIS(20,29)|SOILS(20,8)|CARBON DIOXIDE(19,36)|CORRELATION(19,2)|LIGHT CATION(19,2)|LASER INDUCED BREAKDOWN SPECTROSCOPY(18,132)|ENHANCED ROCK WEATHERING(17,41)|TARGET AREA(16,26)|ORGANIC CARBON(16,3)|SOIL IMPROVEMENT(16,1)|BIOAVAILABLE NUTRIENT QUANTIFICATION(15,1)|SINGLE PLOT(15,1)|MRV(14,16)|CALCULATING HEAVY METAL(14,2)|PATCHWORK SMALLHOLDER FARM(14,1)|SOIL SAMPLE(13,11)|CALIBRATION CURVE(13,10)|INFIELD DEPLOYMENT(13,3)|COVARIANCE COMPREHENSIVE ASSESSMENT(13,1)|INTERSAMPLE HETEROGENEITY COMPREHENSIVE EXAMINATION(13,1)|PELLETIZED SUBSAMPLE RASTERED ANALYSIS(13,1)|HEAVY METAL(12,10)|ROCK(11,5)|IGNITION(11,3)|SOIL HETEROGENEITY(11,3)|COMPOSITIONAL CHARACTERIZATION(11,2)|ECONOMICALLY DISADVANTAGED COMMUNITY(11,1)|PHOSPHORUS P(11,1)|OCEAN ACIDIFICATION(10,2)|PREDICTION MODEL(10,2)|INCENTIVIZE EMISSION AVOIDANCE(10,1)|OCEAN FLORA HEALTH(10,1)|ROBUST MRV FRAMEWORK(10,1)|TOTAL CARBON DIOXIDE(9,6)|AUTOFOCUSING COMPONENT(9,5)|OPTICAL SOURCE(9,5)|AGRICULTURAL SETTING(9,4)|DEPTH INTEGRATED SOIL PROFILE(9,4)|INDUCTIVELY COUPLED PLASMA(9,4)|AQUEOUS METAL(9,3)|CARBON CREDIT GENERATION CREDIBILITY(9,3)|MANAGING STATE(9,3)|GEOLOCATED ZONE SOIL SAMPLING(9,1)|GRADUAL ROCK DISSOLUTION(9,1)|ROCK WEATHERING STATUS(9,1)|CARBON CAPTURE(8,8)|ORGANIC CARBON MEASUREMENT(8,3)|AGRONOMIC COBENEFIT(8,1)|BASALT DISSOLUTION(8,1)|CORAL ECOSYSTEM(8,1)|DISHONEST ACTOR(8,1)|DOMINANT SPECIATION(8,1)|ENHANCE OCEAN ALKALINITY(8,1)|GEOLOCATED ZONE SAMPLING(8,1)|GROUNDWATER RUNOFF(8,1)|INVALUABLE INSIGHT(8,1)|NUTRIENT REQUIREMENT ESTIMATION(8,1)|PREDICTING WEATHERING(8,1)|PULVERIZED ROCK DUST(8,1)|ROCK MINERAL BREAKDOWN(8,1)|SOIL PENETRATION(8,1)|TRADABLE CERTIFICATE(8,1)|ALKALI SILICATE MINERAL(7,3)|EMPIRICALLY DRIVEN MODEL(7,3)|LIGHT COLLECTION OPTICS(7,3)|AGRICULTURAL LAND(7,2)|GRAPHICAL REPRESENTATION(7,2)|AGRICULTURAL SOILS(7,1)|BICARBONATE PRECIPITATION(7,1)|BROAD ELEMENTAL COVERAGE(7,1)|CENTRAL COMPOSITIONAL TENDENCY ASSESSMENT(7,1)|COLLABORATIVE FRAMEWORK(7,1)|FLUORESCENCE SPECTRUM(7,1)|FORESTRY INTERVENTION(7,1)|GEOLOGICAL ATTRIBUTE(7,1)|ICP MS CALIBRATION INTEGRATION(7,1)|RELIABLE CALIBRATION FRAMEWORK(7,1)|ROBUST CALIBRATION(7,1)|ROOT RESPIRATION(7,1)|SOIL SUITABILITY(7,1)|SPATIAL HETEROGENEITY GRANULAR UNDERSTANDING(7,1)|STANDARDIZED REPORTING(7,1)|SYSTEMATIC VARIABILITY(7,1)|TANGIBLE NONVOLATILE PROGRAM CARRIER(7,1)|UNLISTED ITEM(7,1)|WEATHERING OUTCOME(7,1)|ANALYSIS COMPONENT(6,8)|GENERATING CARBON CREDIT(6,4)|DEPTH INTERVAL(6,2)|ELEMENTAL COMPOSITION ANALYSIS(6,2)|KEY CATION(6,2)|MOTOR INSTRUMENT(6,2)|QUANTITATIVE ELEMENTAL ANALYSIS(6,2)|RASTER PATTERN(6,2)|SEED MATTER(6,2)|SOIL COLUMN(6,2)|SUBCOMBINATION(6,2)|SUPPORTING DATA(6,2)|ACIDIC SOIL REMEDIATION(6,1)|ADDRESS CHALLENGING(6,1)|AGRONOMIC BENEFIT(6,1)|BUYER CONCERN(6,1)|CARBON SEQUESTRATION KNOWABILITY(6,1)|CRUCIAL INSIGHT(6,1)|CRUCIAL ISSUE(6,1)|DECISION INFORMATION(6,1)|DEEP AQUIFER(6,1)|DISSOLVE BICARBONATE(6,1)|ELEMENTAL IDENTIFICATION(6,1)|FARMER BURDEN(6,1)|INTEGRATING UNCERTAINTY MODELING(6,1)|MARKUP LANGUAGE(6,1)|MEASUREMENT MISFIT(6,1)|MINERAL CLASSIFICATION(6,1)|MOBIL INSTRUMENT(6,1)|MULTITHREADED PROCESSOR(6,1)|PELLETIZING SOIL(6,1)|POOLED SAMPLE UTILIZATION(6,1)|PRESSED PELLETIZED SUBSAMPLE(6,1)|REPLANT TREE(6,1)|ROCK DUST ARRAY(6,1)|SCRIPT INSTRUCTION(6,1)|SOIL FERTILITY ASSESSMENT(6,1)|SOIL SPATIAL VARIABILITY(6,1)|SUBSURFACE NEAR CROP(6,1)|UNTREATED SEWAGE SLUDGE(6,1)|VERSATILE SAMPLING(6,1)|SOIL ORGANIC CARBON(5,10)|HCO(5,6)|MRV(5,6)|METAL(5,5)|DECISION MAKING INFORMATION(5,3)|FERTILIZER(5,3)|MEASURING CARBON(5,3)|SEA(5,3)|TARGET SAMPLE(5,3)|SAMPLE PROBE(5,2)|3G WIRELESS MODEM(5,1)|4G WIRELESS MODEM(5,1)|ABSENT INCLUSION(5,1)|ALKALINE MINERAL(5,1)|ANALYTICAL ACCURACY(5,1)|BASALT WEATHERING REACTION(5,1)|BICARBONATE DRAW(5,1)|COMPOSITIONAL ANALYSIS(5,1)|COORDINATED FILE(5,1)|COVARIANCE RELATIONSHIP(5,1)|DEMAND FULFILLMENT(5,1)|DEPTH PROFILING(5,1)|DETECTING CARBON DECEPTION(5,1)|DISSOLVED CARBON DOMINANT(5,1)|ECOLOGICAL RISK(5,1)|EXCLUSIVITY TERM(5,1)|FUTURE OBSTACLE(5,1)|GRID ANALYSIS(5,1)|INFIELD ANALYSIS(5,1)|INSTRUCTION INTERPRETATION(5,1)|LASER IRRADIATION(5,1)|MINERAL BICARBONATE(5,1)|MODELING UNCERTAINTY(5,1)|MRV QUALITY(5,1)|NONNORMAL DISTRIBUTION(5,1)|PH AMENDMENT(5,1)|PHYSICAL(5,1)|PLASMA PLUME(5,1)|POOLED SAMPLE ACCURATE MEASUREMENT(5,1)|PRECISE CHARACTERIZATION(5,1)|PROCESSOR FIRMWARE(5,1)|QUANTIFICATION ANALYSIS(5,1)|RAW ROCK SAMPLE(5,1)|REPORT CARBON SEQUESTRATION(5,1)|ROBUST ANALYSIS(5,1)|ROBUST MONITORING(5,1)|SAMPLE HANDING(5,1)|SATELLITE SENSOR(5,1)|SERVER DISTRIBUTION(5,1)|SOIL QUALITY PRECISE ASSESSMENT(5,1)|SOILS TRANSITION(5,1)|SPECTROSCOPY MEASUREMENT(5,1)|TARGET VARIANCE(5,1)|VERIFIABLE CARBON CREDIT(5,1)|WORKFLOW PROPOSITION(5,1)|CARBON DISSOLUTION(4,2)|CENTRALIZED COMPUTING(4,2)|GRAVEL(4,2)|MULTITASKING(4,2)|OPTIMIZATION(4,2)|TRACTOR(4,2)|ADJUSTING ROCK(4,1)|AGGREGATING SOIL SAMPLE(4,1)|ALKALINE SILICATE MINERAL POTENTIAL(4,1)|BASELINE INFORMATION(4,1)|CALCIUM CARBONATE MINERAL(4,1)|CALCULATION REPRESENTATION(4,1)|CARBON BEHAVIOR(4,1)|CARBON CREDIT GENERATION RELIABILITY(4,1)|CARBON CREDIT SALE(4,1)|CARBON DIOXIDE SEQUESTRATION POTENTIAL(4,1)|CARBON MEASUREMENT ISSUE(4,1)|CARBON STORAGE PERMANENCE(4,1)|CARBON UPTAKE(4,1)|CLOUD PROCESSING(4,1)|CLOUD STORAGE(4,1)|COMPUTING ENVIRONMENT(4,1)|DEEP UNDERSTANDING(4,1)|EMBODIED COMPUTER SOFTWARE(4,1)|ENHANCING MEASURE(4,1)|ENSURING STABILITY(4,1)|EXECUTION ENVIRONMENT(4,1)|FLASH MEMORY(4,1)|FOSSIL FUEL COMPANY(4,1)|GEOLOGICAL TIMESCALE(4,1)|INITIATIVE(4,1)|INORGANIC CARBON AQUEOUS SPECIES(4,1)|INSTANTIATION(4,1)|MAJOR AQUEOUS SPECIES(4,1)|MICROHETEROGENEITY(4,1)|MIDDLEWARE COMPONENT(4,1)|MOBILE VEHICLE(4,1)|NET EMISSION(4,1)|ORDINAL TERM(4,1)|ORDINARY MEANING(4,1)|PH RISE(4,1)|PHYTOREMEDIATION(4,1)|POOLED SOIL SAMPLE(4,1)|POOLING SAMPLE(4,1)|PRIMARY FACET(4,1)|QUANTIFYING CARBON CREDIT(4,1)|QUICK ADJUSTMENT(4,1)|ROBOTIC ARM(4,1)|ROCK POWDER(4,1)|SAMPLE PRESENTATION(4,1)|SOIL QUALITY ASSESSMENT(4,1)|SOIL SAMPLING TECHNIQUE ADVANCE(4,1)|SPECIES DISTRIBUTION(4,1)|STANDARDIZED SUBSTRATE(4,1)|TRUSTWORTHINESS(4,1)|VARIABLE FOCUS LENS(4,1)|WIRELESS INTERFACE(4,1)|MACHINE LEARNING(3,3)|SOIL SAMPLE COLLECTION(3,3)|STRATEGY(3,3)|WEB BROWSER(3,3)|STRUCTURED GRID(3,2)|ACCOUNTABILITY(3,1)|AGNOSTIC(3,1)|AGRICULTURAL MACHINERY(3,1)|ANALYSIS REPRESENTATION(3,1)|APPLYING CRUSHED ROCK PRACTICE(3,1)|ARTIFICIALLY GENERATED PROPAGATED SIGNAL(3,1)|ATMOSPHERIC CARBON DIOXIDE(3,1)|AUDITORY FEEDBACK(3,1)|BASELINE DATA(3,1)|CARBON DIOXIDE EMISSION(3,1)|CARBON GAIN(3,1)|CENTURY(3,1)|CHANGING GROUND(3,1)|CLIENT SERVER RELATIONSHIP(3,1)|COLLECTED LIGHT PULSE(3,1)|COMPARABILITY(3,1)|COMPOSITIONAL ARRAY RANGE(3,1)|COMPUTER PROGRAM INSTRUCTION(3,1)|CONSERVATION(3,1)|CREATING CARBON CREDIT(3,1)|DEDUCE(3,1)|DISCRETE REGION(3,1)|DISPLAYING INFORMATION(3,1)|DRONE(3,1)|DUST SAMPLE(3,1)|EMISSION TEST(3,1)|ENHANCED WEATHERING PRACTICE(3,1)|ENVIRONMENTAL ASSESSMENT(3,1)|EQUIVALENT STRUCTURE(3,1)|EXPRESS SUPPORT(3,1)|FACTORING(3,1)|FITTING MULTIVARIATE NORMAL(3,1)|GAME CONSOLE(3,1)| (US20250164404)|What is claimed is:|1. A system for monitoring, reporting, and verification of enhanced rock weathering comprising:| a spectroscopy device comprising an optical source and a detector, wherein the optical source is configured to emit one or more optical signals directed to a target collected from a target area, and the detector is configured to determine spectral measurements of the optical signals collected from the target; and| a data analysis subsystem coupled to the spectroscopy device and configured to:| convert the spectral measurements to data indicating compositional characteristics of the target;| analyze the data indicating compositional characteristics of the target using a plurality of analytical tools; and| provide assessments on carbon dioxide removal and insights on enhanced rock weathering.|2. The system of claim 1, wherein, to convert the spectral measurements to the data indicating compositional characteristics of the target, the data analysis subsystem is further configured to determine a weathering status, evaluate target contents, calculate heavy metal concentration, determine metal ratios in the target, or measure organic carbon in the target.|3. The system of claim 2, wherein, to determine the weathering status, the data analysis subsystem is further configured to determine loss of rock dust by assessing composition of cations in rock dust applied to the target area through the enhanced rock weathering.|4. The system of claim 2, wherein the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals.|5. The system of claim 2, wherein the soil organic carbon is measured based on determining loss of material on ignition.|6. The system of claim 1, wherein the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area.|7. The system of claim 6, further comprising a sampling handing unit configured to identify geolocated zones within the target area from which the pooled sample is collected, wherein the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling.|8. The system of claim 1, wherein, to analyze the data indicating compositional characteristics, the data analysis subsystem is further configured to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS.|9. The system of claim 1, wherein, to provide the assessments on carbon dioxide removal and insights on enhanced rock weathering, the data analysis subsystem is further configured to create a prediction model to provide data support for subsequent implementation of enhanced rock weathering.|10. The system of claim 1, wherein, to provide the assessments on carbon dioxide removal and insights on enhanced rock weathering, the data analysis subsystem is further configured to determine one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.|11. The system of claim 1, wherein the spectroscopy device is a handheld LIBS device.|12. The system of claim 1, wherein the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and wherein the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis.|13. The system of claim 1, wherein the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.|14. A method for monitoring, reporting, and verification of enhanced rock weathering comprising:| emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area;| determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target; and| converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target;| analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools; and| providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.|15. The method of claim 14, wherein converting the spectral measurements comprises one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target.|16. The method of claim 15, wherein determining the weathering status comprises determining loss of rock dust by assessing composition of cations in rock dust applied to the target area through the enhanced rock weathering.|17. The method of claim 14, further comprising identifying geolocated zones within the target area from which the target is collected, wherein the target is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling.|18. The method of claim 14, wherein analyzing the data indicating compositional characteristics comprises performing one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS.|19. The method of claim 14, wherein providing the assessments on carbon dioxide removal and insights on enhanced rock weathering comprises determining one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.|20. The method of claim 14, wherein the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and wherein the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis. (US20250164404)|CROSS REFERENCE TO RELATED APPLICATION|[0001] This application claims the benefit of U.S. Provisional Patent Application No. 63/601,059, titled “System and Method for Enhanced Rock Weathering Monitoring, Reporting, and Verification,” and filed on Nov. 20, 2023, the entire content of which is incorporated by reference herein.|(US20250164404)|TECHNICAL FIELD|[0002] This disclosure relates to compositional characterization techniques, in particular, to optical devices that embody new methodologies for monitoring, reporting, and verification (MRV) of enhanced rock weathering (ERW).|BACKGROUND|[0003] Enhanced rock weathering (ERW) is the practice of applying crushed rocks and silicate minerals to agricultural land. It is a promising scalable and cost-effective carbon dioxide removal (CDR) strategy with significant environmental and agronomic co-benefits. However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions. Most current projects/systems/devices cannot accurately obtain carbon measurement and properly report carbon sequestration. Also, ERW lacks a robust monitoring, reporting, and verification (MRV) framework to address challenging problems such as carbon deception. For example, current MRV practices cannot provide a framework to easily detect and process a fraudulent claim of carbon gains by dishonest actors in the system.|SUMMARY|[0004] To address the aforementioned shortcomings, a method and a system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. The method include using a spectroscopy device to emit one or more optical signals directed to a target collected from a target area and to determine spectral measurements of the optical signals collected from the target. The method also includes using a data analysis subsystem to convert the spectral measurements to data indicating compositional characteristics of the target, analyze the data indicating compositional characteristics of the target using a plurality of analytical tools, and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.|[0005] To convert the spectral measurements to the data indicating compositional characteristics of the target, one or more of the processes, such as determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. To determine the weathering status, loss of rock dust is determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering. To analyze the data indicating compositional characteristics, analytical tools are used to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS. To provide the assessment on carbon dioxide removal and insights on enhanced rock weathering, a prediction model is created to provide data support for subsequent implementation of enhanced rock weathering, and/or one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential are determined.|[0006] In some embodiments, the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals. In some embodiments, the soil organic carbon is measured based on determining the loss of material on ignition. In some embodiments, the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling. In some embodiments, the spectroscopy device is a handheld LIBS device. In some embodiments, the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis. In some embodiments, the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.|[0007] The above and other preferred features, including various novel details of implementation and combination of elements, will now be more particularly described with reference to the accompanying drawings and pointed out in the claims. It will be understood that the particular methods and apparatuses are shown by way of illustration only and not as limitations. As will be understood by those skilled in the art, the principles and features explained herein may be employed in various and numerous embodiments.|(US20250164404)|BRIEF DESCRIPTION OF THE DRAWINGS|[0008] The disclosed embodiments have advantages and features which will be more readily apparent from the detailed description, the appended claims, and the accompanying figures (or drawings). A brief introduction of the figures is below.|[0009] FIG. 1A illustrates a block diagram of an exemplary ERW process.|[0010] FIG. 1B illustrates a graphic representation of the speciation of a dominant form of dissolved carbon.|[0011] FIG. 2A illustrates an overview of an exemplary laser induced breakdown spectroscopy (LIBS)-based data system, according to some embodiments.|[0012] FIG. 2B illustrates an overall diagram of an exemplary LIBS device, according to some embodiments.|[0013] FIG. 3 illustrates a block diagram of exemplary uses of LIBS devices in an MRV process for ERW, according to some embodiments.|[0014] FIG. 4 illustrates a block diagram of exemplary features of LIBS devices and analysis used in MRV for ERW described in the present system, according to some embodiments.|[0015] FIG. 5 illustrates a block diagram of exemplary data analysis and modeling used in the present system, according to some embodiments.|[0016] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments.|[0017] FIG. 7 illustrates a block diagram of an example computer system that may be used in implementing the technology described herein, according to some embodiments.|(US20250164404)|DETAILED DESCRIPTION|[0018] The Figures (FIGs.) and the following description relate to preferred embodiments by way of illustration only. It should be noted that from the following discussion, alternative embodiments of the structures and methods disclosed herein will be readily recognized as viable alternatives that may be employed without departing from the principles of what is claimed.|[0019] Reference will now be made in detail to several embodiments, examples of which are illustrated in the accompanying figures. It is noted that wherever practicable similar or like reference numbers may be used in the figures and may indicate similar or like functionality. The figures depict embodiments of the disclosed system (or method) for purposes of illustration only. One skilled in the art will readily recognize from the following description that alternative embodiments of the structures and methods illustrated herein may be employed without departing from the principles described herein.|Scientific Introduction|ERWA—A Durable Carbon Dioxide Removal Strategy|[0020] Enhanced rock weathering (ERW) is a carbon dioxide removal (CDR) technique where naturally occurring mineral weathering reactions that consume atmospheric CO2 are accelerated. This may be achieved by applying crushed rocks and silicate minerals to agricultural soils. When the gradual rock dissolution or “weathering” occurs, alkaline minerals containing cations, such as calcium and magnesium (Ca2+ and Mg2+) that comprise the silicates, act as a pH amendment to remediate acidic soil on farms. In addition to balancing the pH of the soil, ERW can remove carbon dioxide from the atmosphere and sequester carbon for geological timescales.|[0021] Basalt can be applied to managed land or an agricultural setting (e.g., rice paddies, corn fields, pasture lands) to practice ERW as a CDR strategy at scale. It should be recognized that the approach described herein is crop agnostic and can be generally applicable to any agricultural or managed land. As the dissolution of basalt proceeds, CO2 gas in the soil is converted to dissolved bicarbonate (HCO3−) in groundwater. This occurs due to basalt weathering reactions involving carbonic acid. Carbonic acid (H2O+CO2═H2CO3) is formed naturally in soils by plant respiration. The conversion of dissolved carbonic acid sources to bicarbonate draws CO2 down from the atmosphere.|[0022] FIG. 1A illustrates a block diagram 100 of an exemplary ERW process. Basalt and/or other silicate materials (e.g., crushed rocks or “rock powder”) are applied to the soil and mixed into the subsurface near crops in 102. As the ERW progresses, the carbon dioxide (CO2 gas) from the respiration of roots 104 is converted to bicarbonate (HCO3−) in groundwater, and the CO2 stored in the soil 104 is also leached out of the soil and converted to bicarbonate. The bicarbonate is associated with a rising pH value of soil since the soil becomes less acidic. In this way, CO2 is removed. The silicate material application and CO2 isolation are associated with the deposition and sequestration processes 106, which results in the formation of weathering products in surface and groundwater runoff 108. Multiple enhanced rock weathering experiments have also demonstrated significant agronomic benefits due to improved nutrient supply for crops. Therefore, ERW deployments could aid farmers in regions where fertilizers are scarcely available or unaffordable.|Carbon in Agricultural Setting|[0023] The behavior of carbon in agricultural settings depends on the pH values in the settings. FIG. 1B illustrates a graphic representation 150 of the speciation of a dominant form of dissolved carbon, specifically, a representative calculation for the speciation of dissolved inorganic carbon (DIC). DIC is the sum of the aqueous species of inorganic carbon in a solution, which includes three major aqueous species: CO2, HCO3−, and CO32−. The speciation of DIC is the distribution of these species in a solution. The speciation of DIC can be determined by measuring the pH and total alkalinity of a solution and then using the measured values to calculate the concentrations of the different DIC species.|[0024] To obtain the calculation demonstrating how the behavior of DIC changes with the pH value of soil in FIG. 1B, the pH value of the soil and pore waters of rice paddies is shifted towards pH=7 from ERW. As low pH (i.e., acidic) soils transition to neutral pH (i.e., pH≈7 ), dissolved CO2 is converted to the alkaline dissolved mineral bicarbonate (HCO3−). Near PH=7 bicarbonate is the dominant form of DIC. In other words, based on the shifting of the pH value, CO2 is converted to HCO3− and is not released as gas into the atmosphere.|[0025] Next it is investigated what happens after CO2 is converted to other forms of dissolved inorganic carbon. After the conversion from CO2 to HCO3−, the bicarbonate (HCO3−) percolates into streams and rivers, from where the bicarbonate is delivered to the oceans. This DIC may reside in groundwater within the soil column for decades to centuries. This is an effective removal of carbon dioxide available to the ocean-atmosphere system. The eventual precipitation of bicarbonate as calcium carbonate minerals in deep aquifers or after transport to the ocean stably stores carbon for more than 10,000 years. The delivery of DIC to the ocean in the form of bicarbonate acts to enhance ocean alkalinity, which is vital for the health of ocean flora and fauna. For example, coral ecosystems have been particularly damaged by ocean acidification which is a well-known side effect of climate change. Ocean alkalinity enhancement works to counteract ocean acidification, as shown in 110 of FIG. 1A.|Technical Problems|[0026] It is hard to measure carbon capture. In agricultural and forest environments, many methods have been developed for measuring how much carbon is stored in soil. These methods significantly rely on labor-intensive mass-spectrometer measurements, spectroscopy, satellite-based sensors, and modeling. However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land. These methods cannot accurately evaluate carbon captured and retained in soils. Most current projects/methods cannot successfully quantify the amount of carbon, much less report carbon sequestration and conservation confidently. These schemes do not help address or incentivize emission avoidance and reduction by high-carbon industries (including agriculture).|[0027] Even if the issue of carbon measurement can be solved, there are other challenges such as carbon deception. This is another main challenge related to the “net zero” demand in ecosystems. “Net zero” refers to a situation where an amount of carbon dioxide is removed from the atmosphere after that amount of carbon dioxide emission is generated, resulting in zero increase in net emissions. Thus, gas emission is still generated from human activity (e.g., fossil fuel companies can continue to explore, drill, extract, and burn fossil fuels), but carbon dioxide is taken out of the atmosphere in certain ways in some other places to balance out emissions. However dishonest actors may present during this procedure. For example, like a manufacturer rigging vehicles to cheat on emissions tests, forestry interventions may cut trees and then replant trees to claim carbon gains, i.e., carbon deception. Monitoring, reporting, and verification (MRV) is the process that can account for, communicate, and certify a CDR system's carbon removal over time. Currently, ERW lacks a robust MRV framework to obtain proper knowability of carbon sequestration (e.g., detecting carbon deception) and fill the knowledge gap to fulfill the demand of “net zero.”|[0028] MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved. Some crucial issues in MRV include accurately tracking carbon uptake, ensuring the permanence of carbon storage (e.g., long-time leakage risk), dealing with the variability of the process across different conditions, developing standardized reporting methods that ensure credibility and comparability across projects, etc. For example, there is no feasible way to directly measure the amount of CO2 removed from the atmosphere by ERW, and measuring CO2 in soils and groundwater is inherently challenging due to variability in environmental conditions (e.g., temperature, moisture levels, soil type, microbial activity). Emerging technologies (e.g., remote sensing, advanced soil sampling techniques) and research on effective MRV may help overcome some of the challenges.|Overview|[0029] The present disclosure proposes a novel system and method for performing compositional characterization of soil-rock dust mixtures. In some embodiments, the present system includes laser induced breakdown spectroscopy (LIBS) instruments that embody new MRV methodologies for ERW. LIBS deduces the elemental composition of a sample (e.g., solids, liquids, and gases) from measurements of the spectral line emission emitted by the plasma produced by high-power laser irradiation of the sample. LIBS will be described in further detail below.|[0030] In some embodiments, the proposed workflow as described herein may include four primary facets:| - i. Choose where to sample and measure compositional characteristics of soils;| - ii. Determine how to measure compositional characteristics of the soils using LIBS;| - iii. Analyze LIBS measurements (e.g., based on existing gold-standard measurement techniques); and| - iv. Use post-processing analytical tools to create high-quality, verifiable carbon credits (a tradable certificate used to reduce global greenhouse gas emissions).|[0035] The present disclosure also proposes multiple LIBS devices that may be employed in the field, workstations, or laboratories.|[0036] FIG. 2A illustrates an overview of an exemplary LIBS-based data system 200 that is used to implement the functionalities described herein. In this example, system 200 includes a sample handling unit 202, a LIBS device 204, and a data processing unit 206. System 200 may use sample handling unit 202 to identify locations or zones that target samples (e.g., soil samples) should be collected from (e.g., geolocated zone-based soil sampling). Depending on different quantitative analyses and qualitative analyses to be performed (e.g., as described in FIGS. 3-6), sample handling unit 202 may also be used to instruct LIBS device 204 to obtain specific types of measurements. The present system may further use sample handling unit 202 to ensure the accurate positioning of a sample for optical interaction with LIBS device 204. LIBS device 204 is employed to obtain measurements and analysis data from samples, which will be described in detail in FIG. 2B. The data from LIBS device 204 is further analyzed and modeled by data processing unit 206 for the purpose of monitoring, reporting, and verification, for example, as illustrated in FIG. 5 below. Although only one LIBS device is shown in the example system 200 of FIG. 2A, it is possible that more LIBS devices and/or other units/components may be included in a LIBS-based data system.|[0037] In some embodiments, at least a portion of the data processing unit 206 is part of a computer system (described below in FIG. 7) that is communicatively coupled to LIBS device 204. In other embodiments, at least a portion of the data processing unit 206 may be integrated into LIBS device 204. For example, data processing unit 206 may reside on a standalone computer system to perform advanced compositional analysis based on real-time sample analysis from data acquisition & analysis component 260 of LIBS device 204 (described below in FIG. 2B). Data processing unit 206 together with data acquisition & analysis component 260 form a data analysis subsystem that is responsible for various types of data processing, evaluation, calculation, etc, as described in the present disclosure. When LIBS device 204 is attached to or mounted on a motor instrument (e.g., vehicle, drone), the data analysis subsystem may be integrated into data acquisition onboard the motor instrument for real-time data acquisition and analysis. In some embodiments, at least a portion of the sample handling unit 202 may also be part of an external computer system and/or an integrated part of LIBS device 204. For example, sample handling unit 202 may be designed to use motorized stages or robots to move a sample in a controlled manner and thus is included in or attached to LIBS device 204 for precise sample positioning.|LIBS Device|[0038] LIBS is a rapid chemical analysis technology that uses a short laser pulse to create a micro-plasma on the sample surface. LIBS can be used to detect the presence of various elements in a sample based on directing a high-power emission from a laser onto the sample to form a plasma. The plasma is then analyzed spectroscopically to determine the composition of the sample. The LIBS is often used with a soil penetrating probe to detect heavy metal contamination in soil due to its high sensitivity and sample-free preparation. The LIBS analytical technique offers some other compelling advantages such as fast measurement time (e.g., a few seconds for a single spot analysis), broad elemental coverage (e.g., including, but not limited to, lighter elements such as H, Be, Li, C, N, O, Na, and Mg), versatile sampling protocols that include fast raster of the sample surface and depth profiling, etc.|[0039] The present disclosure proposes new LIBS device(s) used in the MRV process for ERW. In some embodiments, the new LIBS device is a single multi-purpose optical device. In other embodiments, the new LIBS device may include one or more optical devices. Each device can be designed for a single purpose or multiple purposes. The LIBS devices may have various physical components and/or configurations.|[0040] FIG. 2B illustrates an overall block diagram of an exemplary LIBS device 204, which includes some key components such as optical source 254, focusing and light collection optics 256, detector 258, and data acquisition & analysis component 260. These components are depicted merely for illustration, and other components (more or less) may be included in LIBS device 204. For example, sample probe 252 may be part of the LIBS device 204. In some embodiments, LIBS device 204 may use a sample probe 252 (e.g., a soil penetrating probe) to take a sample from a target area that is strategically identified (e.g., on managed land). In response, optical source 254 (e.g., a laser) may generate a high-energy light pulse that is directed onto the sample, and focusing and light collection optics 256 (e.g., lens, mirrors) may focus the light pulse to a specific point on the sample, thereby creating a plasma plume. The focusing and light collection optics 256 may also capture/collect the light pulse/beam to avoid light interference. The collected light pulse is then passed through detector 258 (e.g., spectrometer) to obtain sample measurements (e.g., spectral data). For example, detector 258 may disperse the light pulse into individual wavelengths, determine the intensity of light at each wavelength (e.g., using a charge-coupled device (CCD) or photo-multiplier tube (PMT)), and generate a spectrum that is characteristic of specific elements in the sample.|[0041] Data acquisition & analysis component 260 may include computing hardware such as a central processing unit, memory, and storage, as described in the computer system of FIG. 7. Data acquisition & analysis component 260 is configured to receive the measurement data from detector 258 and perform the elemental composition analysis on the measurement data. In some embodiments, LIBS device 204 may also communicate with an alternative or additional data processing unit (e.g., 206) to perform LIBS analysis and any other elemental identification and quantification analyses. Based on the analysis, a result is generated in 262. For example, the result may be a report or graphical output showing the elemental composition of the sample. Various types of measurements and analyses may be conducted by the data analysis subsystem including data acquisition & analysis component 260 and data processing unit 206, which will be further described below with reference to FIGS. 3-6.|[0042] The present system may deploy one or more improved LIBS devices to implement the disclosed functionalities. For example, the improved LIBS device (e.g., 204) may be equipped, attached, or associated with an autofocusing component to enable consistent, in-focus measurements of samples without moving other optical components. The autofocusing component may be included as a part of a suitable optical assembly that is hand-held, attached to a mobile vehicle, or integrated with a positioning system (e.g., robotic arm, boom, leg, conveyor belt), etc. Using the autofocusing component, spectroscopy measurements can be automatically focused based on a focal length of its optics relative to the target sample. Instead of using certain mechanisms (e.g., mechanical actuators) to change the position of the optical component(s), in some embodiments, the autofocusing component may include a shape changing lens (e.g., variable focus lens) to allow continuous tuning of a focal length and working distance of the autofocusing component relative to a target sample.|Data Acquisition and Evaluation Using LIBS Device|[0043] As discussed above, components 252, 254, 256, 258, and/or 260 of LIBS device 204 may work together with other units of data system 200 to acquire sample data and provide insights about the elemental composition of a sample (e.g., soil sample). In the illustrated embodiment of FIG. 3, one or more LIBS devices 204 may be used to determine weathering status 304, evaluate specific soil contents/elements 306, calculate heavy metal concentration 308, evaluate metal ratios in soils 310, and/or measure soil organic carbon 312. In some embodiments, one or more LIBS devices 200 may also be used to measure and analyze the compositional characteristics of soils, the biological composition of plant and seed matter, and the elemental composition of rock samples.|[0044] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304. In some embodiments, a LIBS-based device may be employed to assess the composition of lighter cations relative to heavier cations in applied rock dust. This composition analysis may be used in determining the weathering status of the rock dust application on agricultural fields, pasture lands, or any other natural environments. Thus, an approach is obtained, for determining the loss of rock dust due to enhanced rock weathering (ERW) for the purpose of monitoring, reporting, and verification (MRV) to create carbon credits.|[0045] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil. This is the estimation of nutrient requirements, factoring in additional nutrients provided by rock dust application. The use of LIBS devices in elemental composition analysis can reduce farmers' burden to apply fertilizers (i.e., NPK nitrogen-phosphorus-potassium) while conducting ERW projects. LIBS allows the quantification of these additional bioavailable nutrients, which become active in the soil column with the breakdown of the rock minerals (e.g., being modified through chemical, physical, or biological interactions with rocks and minerals).|[0046] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW. These elements may include metals such as lead (Pb), mercury (Hg), nickel (ni), etc., and can be found in pesticides, fertilizers, or untreated sewage sludge introduced into the soil. The heavy metal may accumulate in the environment to pose serious health and ecological risks. The disclosed LIBS device may provide insights into the safety considerations of cultivating various crops, for example, providing insights into phytoremediation such as using sunflowers to remove Strontium, which is poisonous metal to most other livings. According to US Environmental Protection Agency (EPA) standards, the bio-availability of metals and dissolved aqueous metals will be needed for calculating heavy metal concentrations.|[0047] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating key metal ratios in soils for ERW 310. In some embodiments, critical metal ratios in soils are assessed using LIBS technology before the implementation of ERW (i.e., before the rock dust application for enhanced weathering). This process can be outlined as follows:| - i. Sample Collection: soil samples are collected from the target area where ERW is planned. These samples represent the current soil composition in the region;| - ii. LIBS Analysis: the collected soil samples are subjected to LIBS analysis. The LIBS device measures the elemental composition of the soil, providing baseline data on the concentrations of various metals being present;| - iii. Trace metal ratios and potential pulverized rock dust field amendments may then be evaluated together to determine if the rock dust is appropriate for application to the field; and | - a. Evaluate environmental concerns,| - b. Evaluate the potential for signal strength in measurements: measuring key metal ratios for MRV process.| - iv. Key Metal Ratios: specific metal ratios of interest, which are known to influence the effectiveness of ERW, are calculated based on the LIBS data. These key metal ratios often include ratios such as calcium to magnesium (Ca/Mg), calcium to potassium (Ca/K), or calcium to sodium (Ca/Na), among others.|[0054] In some embodiments, the calculated key metal ratios are evaluated to determine the suitability of the soil for ERW. An ideal balance of these ratios is typically necessary for optimal carbon capture and weathering outcomes. The assessment results may guide decisions regarding the need for rock dust application and the specific rock dust type required to achieve the desired metal ratios for effective ERW.|[0055] By employing LIBS technology for the evaluation of key metal ratios in soils before rock dust application for enhanced weathering, informed decision-making can be used to ensure that the chosen ERW strategy is tailored to the specific soil composition of the target area. This optimization may also contribute to efficient carbon dioxide removal and MRV.|[0056] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for measuring soil organic carbon 312. A LIBS device can be used to measure soil organic carbon (SOC) levels. The SOC level represents the amount of carbon stored in the form of organic compounds in the soil, and SOC is critical to soil quality and carbon sequestration because it helps store carbon from the atmosphere and contributes to mitigating climate change. By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement. In some embodiments, soil organic carbon measurements may be approximated by the loss of material on ignition (LOI) (e.g., by measuring the weight loss of organic matter content after heating the sample to a high temperature).|LIBS Analysis|[0057] Numerous LIBS analyses may be conducted based on element measurements, calculation, and evaluation. In addition to in-depth soil analysis, when a LIBS device is used to measure the biological composition of plant and seed matter, the LIBS analysis can serve to validate the absence of potential metal accumulation resulting from enhanced weathering processes.|[0058] In some embodiments, a LIBS device may also be used for rock sample analysis, where the elemental composition of raw rock samples from rock quarries or in the field is analyzed. This LIBS analysis may be applied to determine an enhanced weathering potential and a total carbon dioxide removal (CDR) potential. The enhanced weathering potential is the amount of atmospheric carbon dioxide that can be removed and stored through the ERW process (e.g., manual application of rocks or minerals) over a specific period of time. This factor may vary depending on the type of rocks/minerals used in ERW, the surface area available for reaction, environmental conditions (e.g., precipitation, temperature), etc. The total CDR potential is the amount of carbon dioxide that can be removed from the atmosphere in the long term, which depends on the effectiveness of the ERW process.|[0059] In some embodiments, a spectral fluorescence device may be used in combination with LIBS analysis to create a dual system. This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status. In some embodiments, this approach may also be used to help refine soil organic carbon estimates outlined in 312 of FIG. 3. In general, the combination of LIBS and fluorescence may expand and strengthen the LIBS measurement and analysis, e.g., as discussed in FIG. 3.|Beneficial Features of LIBS Device and Analysis|[0060] FIG. 4 illustrates a block diagram 400 of exemplary features of LIBS devices and analysis used in the MRV process for ERW as described in the present system.|[0061] The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402. By aggregating soil samples from various locations within a field, the present system seeks to accurately determine the central compositional tendency and associated dispersion or variance in the soil's elemental composition. As compared to the current techniques, the utilization of pooled samples enables a more robust and representative analysis of the soil's overall composition, contributing to a more precise assessment of soil quality and environmental conditions. The accurate measurement of pooled samples is particularly important to soil fertility assessment, soil quality monitoring, and precision agriculture.|[0062] The present system provides geolocated zone-based soil sampling for target characteristic assessment, as shown in 404. In some embodiments, the present system allows the collection of soil samples from specific geolocated zones within a field. By strategically pooling samples from these distinct zones, the analysis can yield precise data regarding the central tendency and variance of the target characteristic within each zone. This geolocated zone-based sampling approach offers a granular understanding of the spatial heterogeneity, distribution, and variability of the target characteristic, thereby enabling informed decision-making for soil management and ERW applications. Potential future obstacles with a MRV process based on soil heterogeneity may also be addressed by examining measurements at this juncture. In some embodiments, zones may be determined based on soil type, gridded areas, etc. A zone may also be small, predefined regions that include, but are not limited to, a circular region with a predefined radius or a square area with a predefined side length.|[0063] The LIBS device of the present system can be used in rock sample analysis to determine enhanced weathering potential and total carbon dioxide removal (CDR) potential. In particular, the present system may evaluate the carbon dioxide potential of alkaline silicate minerals, as shown in 406. The present system can assess the carbon dioxide potential of alkaline silicate minerals including, but not limited to, basalt, olivine, and wollastonite. These minerals are known for their capacity to sequester carbon dioxide through enhanced weathering processes. In some embodiments, the present system may utilize a LIBS device to analyze the elemental composition of these minerals and determine their specific potential for CDR. By accurately quantifying the CDR potential of alkaline silicate minerals, the present system gains valuable insights into the efficacy of a CDR solution.|[0064] The present system allows systematic preparation of pressed-pelletized subsamples derived from pooled soil samples, as shown in 408. By compressing and pelletizing soil material from each pooled sample, the present system may create a consistent and standardized substrate for LIBS analysis. This process can minimize variations in sample presentation, ensuring reliable and reproducible results during LIBS analysis. This process further streamlines the handling of samples, allowing for an efficient assessment of the central compositional tendency and variance of the target characteristics within the soil, and ultimately enhancing the accuracy of soil quality and environmental assessments.|[0065] The present system further allows grid-based or rastered LIBS sampling for in-depth soil core analysis, as shown in 410. In some embodiments, the present system may conduct grid-based or rastered analyses of the pelletized subsamples, where the LIBS device systematically scans and analyzes discrete regions or points on the pellet surface in a structured grid or raster pattern. This approach enables a comprehensive examination of the intersample heterogeneity (or microheterogeneity) of soil characteristics and the distribution of elemental composition within the subsamples.|[0066] Through this analysis, the present system may achieve a high-resolution understanding of the central compositional tendency and variance of the target characteristics in the soil, and the detailed information may provide invaluable insights into the spatial variability of soil properties, thereby enhancing precision in soil quality assessment and MRV for CDR applications.|[0067] Using rasterized or gridded LIBS sampling can also systematically measure the elemental composition of intact soil cores at various depths. By taking measurements in a prescribed structured grid or raster pattern for LIBS analysis along the length of an intact soil core, the present approach enables precise characterization of the compositional variations with depth. This is particularly beneficial for understanding how soil properties change at different depths within the core, offering crucial insights into subsurface composition and environmental conditions. The present system seeks to assess soil heterogeneity and geological attributes with depth, contributing to informed decisions in ERW applications and MRV techniques.|Device Characteristics and Deployment|[0068] The present system supports specific device characteristics and deployment that are beneficial to the MRV process for ERW. In some embodiments, the present system supports handheld and miniaturized LIBS devices for soil sampling, field-based depth-integrated soil profiling with LIBS and soil auger, and in-field deployment of LIBS technology on motor vehicles, etc.|[0069] The LIBS device described herein can be a handheld device that is portable, easy to operate, and suitable for rapid data acquisition. This handheld device is particularly useful in patchwork small-holder farms (e.g., rice paddies). It is engineered to provide a simplified user interface while maintaining the analytical accuracy and precision required for soil and environmental analysis. Any instantiation of the LIBS device may contain fewer optical sensors than the original, making the device more affordable and lighter. As a result, this LIBS device is adaptive for use in rural, remote, and economically disadvantaged communities. In addition, the miniaturized form of the device enables the present system to perform real-time, in-situ analyses, contributing to timelier and data-driven decision-making processes in agriculture, geology, and environmental science.|[0070] The present system also allows a LIBS device to be combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic. A soil auger is employed to collect soil samples at various depths within the field. These samples are representative of the soil composition at specific depth intervals.|[0071] After and/or during the auguring process, the present system performs LIBS analysis on the collected soil samples. A LIBS device can rapidly and accurately measure the elemental composition of the soil samples, including the concentration of the target characteristic of interest. The present system may then integrate the LIBS data obtained from each depth interval to construct a depth-integrated soil profile of the target characteristic. This profile provides a comprehensive understanding of how the target characteristic varies with depth within the soil.|[0072] A LIBS device/instrument can be deployed in different ways. In some embodiments, the present system supports in-field deployment of LIBS technology on motor vehicles. LIBS is integrated into motor vehicles, such as tractors or other agricultural machinery, for in-field deployment. The present system seamlessly integrates LIBS instrumentation into the design of motor vehicles used for field operations, such as tractors.|[0073] The LIBS device can be securely mounted, ensuring stability during vehicle movement. The LIBS device may operate in real time as the motor vehicle traverses the field. The LIBS device continuously analyzes the soil or other target materials as the vehicle moves, providing instant elemental composition data. The present system may collect LIBS-generated data and integrate the data into a data acquisition (DAQ) onboard the vehicle, allowing for real-time decision-making based on soil or material composition. A vehicle operator can use the LIBS data to make immediate adjustments to field operations for any ERW-related purpose, such as varying fertilizer application rates or adjusting rock dust application rates based on the in-field analysis. The present system may log the LIBS data, providing a detailed record of the soil or material composition across the field for subsequent analysis and optimization.|[0074] In some embodiments, the present system may support other deployment methods. For example, one or more LIBS devices may be integrated into drones, underwater vehicles/amphibious, or other mobil instruments.|Data Analysis and Modeling|[0075] FIG. 5 illustrates a block diagram 500 of exemplary features of data analysis and modeling used in the present system. As depicted in FIG. 5, the data analysis and modeling 502 of the present system may be featured with various analytical tools such as multivariate distribution modeling for cation covariance analysis 504, empirical modeling for weathering prediction and carbon credit creation 506, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data 508, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS 510, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV 512. In some embodiments, these data analyses and modeling may be performed at least by data processing unit 206 in combination with data acquisition & analysis component 260 as shown in FIGS. 2A and 2B (i.e., data analysis subsystem).|[0076] The present system provides multivariate distribution modeling for cation covariance analysis, as shown in 504. In some embodiments, the LIBS data can be leveraged for analyzing and modeling the covariance relationships among key cations in soil including, but not limited to, titanium, calcium, sodium, magnesium, potassium, phosphorous, and nitrogen. In some embodiments, the present system entails fitting multivariate normal or non-normal distributions to the data obtained through LIBS measurements.|[0077] Multivariate distribution fitting allows for the comprehensive assessment of the covariance and correlations between key cations in soil. It provides valuable insights into the simultaneous variations and relationships among these elements, contributing to a deep understanding of soil composition and baseline information required for MRV. The present system uses LIBS to provide dense and rapid enough data to find systematic variances in soil heterogeneity within any given field, pasture, agricultural setting, or any other natural setting.|[0078] In some embodiments, the present system may apply the quantitative elemental analysis approach as described in Sobron, titled “non-linear methods for quantitative elemental analysis and mineral classification using laser-induced breakdown spectroscopy (LIBS),” U.S. patent application Ser. No. 15/998,391, which is hereby incorporated by reference in its entirety.|[0079] In some embodiments, the present system supports empirical modeling for weathering prediction and carbon credit creation, as shown in 406. That is, data collected in the present system can be leveraged to develop an empirically driven model for predicting the weathering of rock dust applied to fields and providing suggestions and instructions for subsequent ERW implementation.|[0080] The empirical model may help the monitoring, reporting, and verification (MRV) process, which aims at quantifying the carbon capture potential resulting from enhanced weathering practices. By using dense, LIBS-generated data to create a predictive model, it becomes possible to monitor and report on the efficiency of carbon capture using regression-based and/or machine-learning methods. As a result, the time between data collection and sales for creating carbon credits may be reduced. The empirically driven model therefore facilitates accurate and data-driven MRV processes while incentivizing an easy switch to practices where carbon credits may be created through ERW. For example, when structure a predictive model, the present system may use mineral type, application rate, surface area of mineral, climate data, and environmental carbon dioxide concentration as input parameters of the model. The present system may calculate the weathering rate based on the environmental conditions and mineral properties, calculate the sequestration of carbon dioxide, and use weathering rate equations to predict how much carbon dioxide may be captured within a specific area over a specific timeframe. The present system may also calculate the total carbon dioxide removal rate to estimate global or regional carbon dioxide sequestration potential.|[0081] To ensure accuracy and precision, in some embodiments, the present system may calibrate the LIBS device using high-precision measurements obtained from ICP-MS, as shown in 508.|[0082] ICP-MS represents a well-established and highly accurate analytical technique, known for its exceptional precision in measuring elemental composition. By calibrating the LIBS device against ICP-MS data, the present system may establish a robust and reliable calibration framework. This calibration method may serve to validate and fine-tune the LIBS measurements, ensuring accuracy and traceability to a gold standard in elemental analysis.|[0083] The integration of ICP-MS calibration in the present system enhances the trustworthiness and consistency of LIBS measurements, and the enhanced measurements may be suitable for a wide range of ERW applications for MRV. This calibration approach boosts the credibility of LIBS technology in scientific research and regulatory compliance (e.g., metals contamination according to EPA standards).|[0084] The present system supports the construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, as shown in 510. In some embodiments, the present system may use known mixtures of soil and rock dust to create calibration curves. With a soil sample and rock dust sample that have already been characterized via ICP-MS or other analytical techniques, the present system can obtain known mixtures such that the rock dust comprises a known percentage of the weight of a newly created sample. By testing many mixed samples using LIBS with an array of rock dust ranging from 0 to 100% weight by mass, the present system can determine a series of calibration curves. These curves may fit the compositional characteristics of a particular soil type-rock dust combination. The present system may then store the data for soil type-rock dust combinations, creating a large database of possible LIBS spectral signals for a range of possible compositional arrays. With a sufficiently large database, the present system can apply one or more regression-based, machine-learning-based tools, and principal component analysis to select the most optimal calibration curve for new measurement(s).|[0085] Here, the present system aims to strengthen the credibility of carbon credit generation. In some embodiments, the present system may use the misfit of measurements to known calibration curves to quantify measurement uncertainty, so that carbon credit sales effectively incorporate potential variations in carbon capture into pricing structures.|[0086] In some embodiments, the present system supports collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV, as shown in 512. In other words, ICP-MS and LIBS are used collaboratively to spot-check and validate the empirically driven model developed for CDR MRV. This process ensures that the model accurately reflects the carbon capture and sequestration processes in real-world applications, enhancing the reliability of carbon credit generation. The present system may also use the same collaborative framework to generate uncertainty models when upscaling the sample area for MRV. To upscale the sample area for MRV, test plots are used to make projections for larger fields, and/or several fields are used to project CDR for a region, etc. By systematically assessing variations and uncertainties using ICP-MS and LIBS data, these models provide insights into the potential variability in carbon capture estimates as the sample area is expanded. This information is essential for accurately quantifying carbon credits and assuaging buyers' concerns about the quality of carbon credits. The information is also crucial to assess the quality of MRV.|[0087] The present system aims to strengthen the credibility of carbon credit generation and improve informed decision-making in ERW-related land management. By integrating uncertainty modeling, the present system enhances its ability to account for variations in carbon capture and carbon dioxide removal potential and provides a comprehensive assessment of carbon dioxide removal efforts. The present system may enhance the credibility of carbon credit generation while providing transparency and accountability in environmental initiatives.|Flowchart|[0088] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments. Method 600 may be implemented using a LIBS-based data system 200, as shown in FIGS. 2A and 2B. A spectroscopy device (e.g., LIBS device 204) is used to obtain measurements from a target sample. At step 602, the spectroscopy device (e.g., using optical source 254) emits one or more optical signals directed to a target collected from a target area (e.g., managed field or other agricultural settings). At step 604, the spectroscopy device (e.g., using detector 258) determines spectral measurements of the optical signals collected from the target. The target can be a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified (e.g., by sample handing unit 202) from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered LIBS sampling.|[0089] As shown in FIGS. 2A and 2B, a data analysis subsystem (e.g., including data processing unit 206 and data acquisition & analysis component 260) is communicatively coupled to the spectroscopy device (e.g., LIBS device 204). At step 606, the data analysis subsystem is configured to convert the spectral measurements to data indicating compositional characteristics of the target, which includes at least one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. For example, to determine the weathering status, loss of rock dust may be determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering.|[0090] The data analysis subsystem is then configured to analyze the data indicating compositional characteristics of the target using a plurality of analytical tools at step 608, and provide assessment on carbon dioxide removal and insights on enhanced rock weathering at step 610. In some embodiments, to analyze the compositional data, the data analysis subsystem uses various analytical tools to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision ICP-MS data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS, etc. To provide the assessment, the data analysis subsystem may also calculate one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.|Computer Implementation|[0091] In some examples, some or all of the processing described above can be carried out on a personal computing device, on one or more centralized computing devices, or via cloud-based processing by one or more servers. Some types of processing can occur on one device and other types of processing can occur on another device. Some or all of the data described above can be stored on a personal computing device, in data storage hosted on one or more centralized computing devices, and/or via cloud-based storage. Some data can be stored in one location and other data can be stored in another location. In some examples, quantum computing can be used, and/or functional programming languages can be used. Electrical memory, such as flash-based memory, can be used.|[0092] FIG. 7 is a block diagram of an example computer system 700 that may be used in implementing the technology described herein. General-purpose computers, network appliances, mobile devices, or other electronic systems may also include at least portions of the system 700. The system 700 includes a processor 710, a memory 720, a storage device 730, and an input/output device 740. Each of the components 710, 720, 730, and 740 may be interconnected, for example, using a system bus 750. The processor 710 is capable of processing instructions for execution within the system 700. In some implementations, the processor 710 is single-threaded. In some implementations, the processor 710 is a multi-threaded processor. The processor 710 is capable of processing instructions stored in the memory 720 or on the storage device 730.|[0093] Memory 720 stores information within the system 700. In some implementations, the memory 720 is a non-transitory computer-readable medium. In some implementations, the memory 720 is a volatile memory unit. In some implementations, the memory 720 is a non-volatile memory unit.|[0094] The storage device 730 is capable of providing mass storage for the system 700. In some implementations, the storage device 730 is a non-transitory computer-readable medium. In various implementations, the storage device 730 may include, for example, a hard disk device, an optical disk device, a solid-state drive, a flash drive, or some other large-capacity storage device. For example, the storage device may store long-term data (e.g., database data, file system data, etc.). The input/output device 740 provides input/output operations for the system 700. In some implementations, the input/output device 740 may include one or more network interface devices, e.g., an Ethernet card, a serial communication device, e.g., an RS-232 port, and/or a wireless interface device, e.g., an 802.11 card, a 3G wireless modem, or a 4G wireless modem. In some implementations, the input/output device may include driver devices configured to receive input data and send output data to other input/output devices, e.g., keyboard, printer, and display devices 760. In some examples, mobile computing devices, mobile communication devices, and other devices may be used.|[0095] In some implementations, at least a portion of the approaches described above may be realized by instructions that upon execution cause one or more processing devices to carry out the processes and functions described above. Such instructions may include, for example, interpreted instructions such as script instructions, executable code, or other instructions stored in a non-transitory computer-readable medium. The storage device 730 may be implemented in a distributed way over a network, such as a server farm or a set of widely distributed servers, or may be implemented in a single computing device.|[0096] Although an example processing system has been described in FIG. 7, embodiments of the subject matter, functional operations, and processes described in this specification can be implemented in other types of digital electronic circuitry, in tangibly embodied computer software or firmware, in computer hardware, including the structures disclosed in this specification and their structural equivalents, or in combinations of one or more of them. Embodiments of the subject matter described in this specification can be implemented as one or more computer programs, i.e., one or more modules of computer program instructions encoded on a tangible nonvolatile program carrier for execution by, or to control the operation of, data processing apparatus. Alternatively or in addition, the program instructions can be encoded on an artificially generated propagated signal, e.g., a machine-generated electrical, optical, or electromagnetic signal that is generated to encode information for transmission to a suitable receiver apparatus for execution by a data processing apparatus. The computer storage medium can be a machine-readable storage device, a machine-readable storage substrate, a random or serial access memory device, or a combination of one or more of them.|[0097] The term “system” may encompass all kinds of apparatus, devices, and machines for processing data, including by way of example a programmable processor, a computer, or multiple processors or computers. A processing system may include special-purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit). A processing system may include, in addition to hardware, code that creates an execution environment for the computer program in question, e.g., code that constitutes processor firmware, a protocol stack, a database management system, an operating system, or a combination of one or more of them.|[0098] A computer program (which may also be referred to or described as a program, software, a software application, a module, a software module, a script, or code) can be written in any form of programming language, including compiled or interpreted languages, or declarative or procedural languages, and it can be deployed in any form, including as a standalone program or as a module, component, subroutine, or other unit suitable for use in a computing environment. A computer program may, but need not, correspond to a file in a file system. A program can be stored in a portion of a file that holds other programs or data (e.g., one or more scripts stored in a markup language document), in a single file dedicated to the program in question, or in multiple coordinated files (e.g., files that store one or more modules, sub programs, or portions of code). A computer program can be deployed to be executed on one computer or on multiple computers that are located at one site or distributed across multiple sites and interconnected by a communication network.|[0099] The processes and logic flows described in this specification can be performed by one or more programmable computers executing one or more computer programs to perform functions by operating on input data and generating output. The processes and logic flows can also be performed by, and apparatus can also be implemented as, special purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit).|[0100] Computers suitable for the execution of a computer program can include, by way of example, general or special purpose microprocessors or both, or any other kind of central processing unit. Generally, a central processing unit will receive instructions and data from a read-only memory, a random access memory, or both. A computer generally includes a central processing unit for performing or executing instructions and one or more memory devices for storing instructions and data. Generally, a computer will also include, or be operatively coupled to receive data from or transfer data to, or both, one or more mass storage devices for storing data, e.g., magnetic, magneto-optical disks, or optical disks. However, a computer need not have such devices. Moreover, a computer can be embedded in another device, e.g., a mobile telephone, a personal digital assistant (PDA), a mobile audio or video player, a game console, a Global Positioning System (GPS) receiver, or a portable storage device (e.g., a universal serial bus (USB) flash drive), to name just a few.|[0101] Computer-readable media suitable for storing computer program instructions and data include all forms of non-volatile memory, media, and memory devices, including by way of example semiconductor memory devices, e.g., EPROM, EEPROM, and flash memory devices; magnetic disks, e.g., internal hard disks or removable disks; magneto-optical disks; and CD-ROM and DVD-ROM disks. The processor and the memory can be supplemented by, or incorporated in special-purpose logic circuitry.|[0102] To provide for interaction with a user, embodiments of the subject matter described in this specification can be implemented on a computer having a display device, e.g., a CRT (cathode ray tube) or LCD (liquid crystal display) monitor, for displaying information to the user and a keyboard and a pointing device, e.g., a mouse or a trackball, by which the user can provide input to the computer. Other kinds of devices can be used to provide for interaction with a user as well; for example, feedback provided to the user can be any form of sensory feedback, e.g., visual feedback, auditory feedback, or tactile feedback; and input from the user can be received in any form, including acoustic, speech, or tactile input. In addition, a computer can interact with a user by sending documents to and receiving documents from a device that is used by the user; for example, by sending web pages to a web browser on a user's user device in response to requests received from the web browser.|[0103] Embodiments of the subject matter described in this specification can be implemented in a computing system that includes a back-end component, e.g., as a data server, or that includes a middleware component, e.g., an application server, or that includes a front-end component, e.g., a client computer having a graphical user interface or a Web browser through which a user can interact with an implementation of the subject matter described in this specification, or any combination of one or more such back end, middleware, or front end components. The components of the system can be interconnected by any form or medium of digital data communication, e.g., a communication network. Examples of communication networks include a local area network (“LAN”) and a wide area network (“WAN”), e.g., the Internet.|[0104] The computing system can include clients and servers. A client and server are generally remote from each other and typically interact through a communication network. The relationship between client and server arises by virtue of computer programs running on the respective computers and having a client-server relationship with each other.|[0105] While this specification contains many specific implementation details, these should not be construed as limitations on the scope of what may be claimed, but rather as descriptions of features that may be specific to particular embodiments. Certain features that are described in this specification in the context of separate embodiments can also be implemented in combination in a single embodiment. Conversely, various features that are described in the context of a single embodiment can also be implemented in multiple embodiments separately or in any suitable sub-combination. Moreover, although features may be described above as acting in certain combinations and even initially claimed as such, one or more features from a claimed combination can in some cases be excised from the combination, and the claimed combination may be directed to a sub-combination or variation of a sub-combination.|[0106] Similarly, while operations are depicted in the drawings in a particular order, this should not be understood as requiring that such operations be performed in the particular order shown or in sequential order, or that all illustrated operations be performed, to achieve desirable results. In certain circumstances, multitasking and parallel processing may be advantageous. Moreover, the separation of various system components in the embodiments described above should not be understood as requiring such separation in all embodiments, and it should be understood that the described program components and systems can generally be integrated together in a single software product or packaged into multiple software products.|[0107] Particular embodiments of the subject matter have been described. Other embodiments are within the scope of the following claims. For example, the actions recited in the claims can be performed in a different order and still achieve desirable results. As one example, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In certain implementations, multitasking and parallel processing may be advantageous. Other steps or stages may be provided, or steps or stages may be eliminated, from the described processes. Accordingly, other implementations are within the scope of the following claims.|Terminology|[0108] The phraseology and terminology used herein are for the purpose of description and should not be regarded as limiting.|[0109] The term “approximately”, the phrase “approximately equal to”, and other similar phrases, as used in the specification and the claims (e.g., “X has a value of approximately Y” or “X is approximately equal to Y”), should be understood to mean that one value (X) is within a predetermined range of another value (Y). The predetermined range may be plus or minus 20%, 10%, 5%, 3%, 1%, 0.1%, or less than 0.1%, unless otherwise indicated.|[0110] The indefinite articles “a” and “an,” as used in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.” The phrase “and/or,” as used in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Multiple elements listed with “and/or” should be construed in the same fashion, i.e., “one or more” of the elements so conjoined. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, a reference to “A and/or B”, when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A only (optionally including elements other than B); in another embodiment, to B only (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.|[0111] As used in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law.|[0112] As used in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.|[0113] The use of “including,” “comprising,” “having,” “containing,” “involving,” and variations thereof, is meant to encompass the items listed thereafter and additional items.|[0114] Use of ordinal terms such as “first,” “second,” “third,” etc., in the claims to modify a claim element does not by itself connote any priority, precedence, or order of one claim element over another or the temporal order in which acts of a method are performed. Ordinal terms are used merely as labels to distinguish one claim element having a certain name from another element having a same name (but for use of the ordinal term), to distinguish the claim elements.|[0115] Each numerical value presented herein, for example, in a table, a chart, or a graph, is contemplated to represent a minimum value or a maximum value in a range for a corresponding parameter. Accordingly, when added to the claims, the numerical value provides express support for claiming the range, which may lie above or below the numerical value, in accordance with the teachings herein. Absent inclusion in the claims, each numerical value presented herein is not to be considered limiting in any regard.|[0116] The terms and expressions employed herein are used as terms and expressions of description and not of limitation, and there is no intention, in the use of such terms and expressions, of excluding any equivalents of the features shown and described or portions thereof. In addition, having described certain embodiments of the invention, it will be apparent to those of ordinary skill in the art that other embodiments incorporating the concepts disclosed herein may be used without departing from the spirit and scope of the invention. The features and functions of the various embodiments may be arranged in various combinations and permutations, and all are considered to be within the scope of the disclosed invention. Accordingly, the described embodiments are to be considered in all respects as only illustrative and not restrictive. Furthermore, the configurations, materials, and dimensions described herein are intended as illustrative and in no way limiting. Similarly, although physical explanations have been provided for explanatory purposes, there is no intent to be bound by any particular theory or mechanism, or to limit the claims in accordance therewith. (US20250164404)|CROSS REFERENCE TO RELATED APPLICATION|[0001] This application claims the benefit of U.S. Provisional Patent Application No. 63/601,059, titled “System and Method for Enhanced Rock Weathering Monitoring, Reporting, and Verification,” and filed on Nov. 20, 2023, the entire content of which is incorporated by reference herein.|(US20250164404)|TECHNICAL FIELD|[0002] This disclosure relates to compositional characterization techniques, in particular, to optical devices that embody new methodologies for monitoring, reporting, and verification (MRV) of enhanced rock weathering (ERW).|BACKGROUND|[0003] Enhanced rock weathering (ERW) is the practice of applying crushed rocks and silicate minerals to agricultural land. It is a promising scalable and cost-effective carbon dioxide removal (CDR) strategy with significant environmental and agronomic co-benefits. However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions. Most current projects/systems/devices cannot accurately obtain carbon measurement and properly report carbon sequestration. Also, ERW lacks a robust monitoring, reporting, and verification (MRV) framework to address challenging problems such as carbon deception. For example, current MRV practices cannot provide a framework to easily detect and process a fraudulent claim of carbon gains by dishonest actors in the system.|SUMMARY|[0004] To address the aforementioned shortcomings, a method and a system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. The method include using a spectroscopy device to emit one or more optical signals directed to a target collected from a target area and to determine spectral measurements of the optical signals collected from the target. The method also includes using a data analysis subsystem to convert the spectral measurements to data indicating compositional characteristics of the target, analyze the data indicating compositional characteristics of the target using a plurality of analytical tools, and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.|[0005] To convert the spectral measurements to the data indicating compositional characteristics of the target, one or more of the processes, such as determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. To determine the weathering status, loss of rock dust is determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering. To analyze the data indicating compositional characteristics, analytical tools are used to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS. To provide the assessment on carbon dioxide removal and insights on enhanced rock weathering, a prediction model is created to provide data support for subsequent implementation of enhanced rock weathering, and/or one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential are determined.|[0006] In some embodiments, the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals. In some embodiments, the soil organic carbon is measured based on determining the loss of material on ignition. In some embodiments, the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling. In some embodiments, the spectroscopy device is a handheld LIBS device. In some embodiments, the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis. In some embodiments, the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.|[0007] The above and other preferred features, including various novel details of implementation and combination of elements, will now be more particularly described with reference to the accompanying drawings and pointed out in the claims. It will be understood that the particular methods and apparatuses are shown by way of illustration only and not as limitations. As will be understood by those skilled in the art, the principles and features explained herein may be employed in various and numerous embodiments.|(US20250164404)|BRIEF DESCRIPTION OF THE DRAWINGS|[0008] The disclosed embodiments have advantages and features which will be more readily apparent from the detailed description, the appended claims, and the accompanying figures (or drawings). A brief introduction of the figures is below.|[0009] FIG. 1A illustrates a block diagram of an exemplary ERW process.|[0010] FIG. 1B illustrates a graphic representation of the speciation of a dominant form of dissolved carbon.|[0011] FIG. 2A illustrates an overview of an exemplary laser induced breakdown spectroscopy (LIBS)-based data system, according to some embodiments.|[0012] FIG. 2B illustrates an overall diagram of an exemplary LIBS device, according to some embodiments.|[0013] FIG. 3 illustrates a block diagram of exemplary uses of LIBS devices in an MRV process for ERW, according to some embodiments.|[0014] FIG. 4 illustrates a block diagram of exemplary features of LIBS devices and analysis used in MRV for ERW described in the present system, according to some embodiments.|[0015] FIG. 5 illustrates a block diagram of exemplary data analysis and modeling used in the present system, according to some embodiments.|[0016] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments.|[0017] FIG. 7 illustrates a block diagram of an example computer system that may be used in implementing the technology described herein, according to some embodiments.|(US20250164404)|DETAILED DESCRIPTION|[0018] The Figures (FIGs.) and the following description relate to preferred embodiments by way of illustration only. It should be noted that from the following discussion, alternative embodiments of the structures and methods disclosed herein will be readily recognized as viable alternatives that may be employed without departing from the principles of what is claimed.|[0019] Reference will now be made in detail to several embodiments, examples of which are illustrated in the accompanying figures. It is noted that wherever practicable similar or like reference numbers may be used in the figures and may indicate similar or like functionality. The figures depict embodiments of the disclosed system (or method) for purposes of illustration only. One skilled in the art will readily recognize from the following description that alternative embodiments of the structures and methods illustrated herein may be employed without departing from the principles described herein.|Scientific Introduction|ERWA—A Durable Carbon Dioxide Removal Strategy|[0020] Enhanced rock weathering (ERW) is a carbon dioxide removal (CDR) technique where naturally occurring mineral weathering reactions that consume atmospheric CO2 are accelerated. This may be achieved by applying crushed rocks and silicate minerals to agricultural soils. When the gradual rock dissolution or “weathering” occurs, alkaline minerals containing cations, such as calcium and magnesium (Ca2+ and Mg2+) that comprise the silicates, act as a pH amendment to remediate acidic soil on farms. In addition to balancing the pH of the soil, ERW can remove carbon dioxide from the atmosphere and sequester carbon for geological timescales.|[0021] Basalt can be applied to managed land or an agricultural setting (e.g., rice paddies, corn fields, pasture lands) to practice ERW as a CDR strategy at scale. It should be recognized that the approach described herein is crop agnostic and can be generally applicable to any agricultural or managed land. As the dissolution of basalt proceeds, CO2 gas in the soil is converted to dissolved bicarbonate (HCO3−) in groundwater. This occurs due to basalt weathering reactions involving carbonic acid. Carbonic acid (H2O+CO2═H2CO3) is formed naturally in soils by plant respiration. The conversion of dissolved carbonic acid sources to bicarbonate draws CO2 down from the atmosphere.|[0022] FIG. 1A illustrates a block diagram 100 of an exemplary ERW process. Basalt and/or other silicate materials (e.g., crushed rocks or “rock powder”) are applied to the soil and mixed into the subsurface near crops in 102. As the ERW progresses, the carbon dioxide (CO2 gas) from the respiration of roots 104 is converted to bicarbonate (HCO3−) in groundwater, and the CO2 stored in the soil 104 is also leached out of the soil and converted to bicarbonate. The bicarbonate is associated with a rising pH value of soil since the soil becomes less acidic. In this way, CO2 is removed. The silicate material application and CO2 isolation are associated with the deposition and sequestration processes 106, which results in the formation of weathering products in surface and groundwater runoff 108. Multiple enhanced rock weathering experiments have also demonstrated significant agronomic benefits due to improved nutrient supply for crops. Therefore, ERW deployments could aid farmers in regions where fertilizers are scarcely available or unaffordable.|Carbon in Agricultural Setting|[0023] The behavior of carbon in agricultural settings depends on the pH values in the settings. FIG. 1B illustrates a graphic representation 150 of the speciation of a dominant form of dissolved carbon, specifically, a representative calculation for the speciation of dissolved inorganic carbon (DIC). DIC is the sum of the aqueous species of inorganic carbon in a solution, which includes three major aqueous species: CO2, HCO3−, and CO32−. The speciation of DIC is the distribution of these species in a solution. The speciation of DIC can be determined by measuring the pH and total alkalinity of a solution and then using the measured values to calculate the concentrations of the different DIC species.|[0024] To obtain the calculation demonstrating how the behavior of DIC changes with the pH value of soil in FIG. 1B, the pH value of the soil and pore waters of rice paddies is shifted towards pH=7 from ERW. As low pH (i.e., acidic) soils transition to neutral pH (i.e., pH≈7 ), dissolved CO2 is converted to the alkaline dissolved mineral bicarbonate (HCO3−). Near PH=7 bicarbonate is the dominant form of DIC. In other words, based on the shifting of the pH value, CO2 is converted to HCO3− and is not released as gas into the atmosphere.|[0025] Next it is investigated what happens after CO2 is converted to other forms of dissolved inorganic carbon. After the conversion from CO2 to HCO3−, the bicarbonate (HCO3−) percolates into streams and rivers, from where the bicarbonate is delivered to the oceans. This DIC may reside in groundwater within the soil column for decades to centuries. This is an effective removal of carbon dioxide available to the ocean-atmosphere system. The eventual precipitation of bicarbonate as calcium carbonate minerals in deep aquifers or after transport to the ocean stably stores carbon for more than 10,000 years. The delivery of DIC to the ocean in the form of bicarbonate acts to enhance ocean alkalinity, which is vital for the health of ocean flora and fauna. For example, coral ecosystems have been particularly damaged by ocean acidification which is a well-known side effect of climate change. Ocean alkalinity enhancement works to counteract ocean acidification, as shown in 110 of FIG. 1A.|Technical Problems|[0026] It is hard to measure carbon capture. In agricultural and forest environments, many methods have been developed for measuring how much carbon is stored in soil. These methods significantly rely on labor-intensive mass-spectrometer measurements, spectroscopy, satellite-based sensors, and modeling. However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land. These methods cannot accurately evaluate carbon captured and retained in soils. Most current projects/methods cannot successfully quantify the amount of carbon, much less report carbon sequestration and conservation confidently. These schemes do not help address or incentivize emission avoidance and reduction by high-carbon industries (including agriculture).|[0027] Even if the issue of carbon measurement can be solved, there are other challenges such as carbon deception. This is another main challenge related to the “net zero” demand in ecosystems. “Net zero” refers to a situation where an amount of carbon dioxide is removed from the atmosphere after that amount of carbon dioxide emission is generated, resulting in zero increase in net emissions. Thus, gas emission is still generated from human activity (e.g., fossil fuel companies can continue to explore, drill, extract, and burn fossil fuels), but carbon dioxide is taken out of the atmosphere in certain ways in some other places to balance out emissions. However dishonest actors may present during this procedure. For example, like a manufacturer rigging vehicles to cheat on emissions tests, forestry interventions may cut trees and then replant trees to claim carbon gains, i.e., carbon deception. Monitoring, reporting, and verification (MRV) is the process that can account for, communicate, and certify a CDR system's carbon removal over time. Currently, ERW lacks a robust MRV framework to obtain proper knowability of carbon sequestration (e.g., detecting carbon deception) and fill the knowledge gap to fulfill the demand of “net zero.”|[0028] MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved. Some crucial issues in MRV include accurately tracking carbon uptake, ensuring the permanence of carbon storage (e.g., long-time leakage risk), dealing with the variability of the process across different conditions, developing standardized reporting methods that ensure credibility and comparability across projects, etc. For example, there is no feasible way to directly measure the amount of CO2 removed from the atmosphere by ERW, and measuring CO2 in soils and groundwater is inherently challenging due to variability in environmental conditions (e.g., temperature, moisture levels, soil type, microbial activity). Emerging technologies (e.g., remote sensing, advanced soil sampling techniques) and research on effective MRV may help overcome some of the challenges.|Overview|[0029] The present disclosure proposes a novel system and method for performing compositional characterization of soil-rock dust mixtures. In some embodiments, the present system includes laser induced breakdown spectroscopy (LIBS) instruments that embody new MRV methodologies for ERW. LIBS deduces the elemental composition of a sample (e.g., solids, liquids, and gases) from measurements of the spectral line emission emitted by the plasma produced by high-power laser irradiation of the sample. LIBS will be described in further detail below.|[0030] In some embodiments, the proposed workflow as described herein may include four primary facets:| - i. Choose where to sample and measure compositional characteristics of soils;| - ii. Determine how to measure compositional characteristics of the soils using LIBS;| - iii. Analyze LIBS measurements (e.g., based on existing gold-standard measurement techniques); and| - iv. Use post-processing analytical tools to create high-quality, verifiable carbon credits (a tradable certificate used to reduce global greenhouse gas emissions).|[0035] The present disclosure also proposes multiple LIBS devices that may be employed in the field, workstations, or laboratories.|[0036] FIG. 2A illustrates an overview of an exemplary LIBS-based data system 200 that is used to implement the functionalities described herein. In this example, system 200 includes a sample handling unit 202, a LIBS device 204, and a data processing unit 206. System 200 may use sample handling unit 202 to identify locations or zones that target samples (e.g., soil samples) should be collected from (e.g., geolocated zone-based soil sampling). Depending on different quantitative analyses and qualitative analyses to be performed (e.g., as described in FIGS. 3-6), sample handling unit 202 may also be used to instruct LIBS device 204 to obtain specific types of measurements. The present system may further use sample handling unit 202 to ensure the accurate positioning of a sample for optical interaction with LIBS device 204. LIBS device 204 is employed to obtain measurements and analysis data from samples, which will be described in detail in FIG. 2B. The data from LIBS device 204 is further analyzed and modeled by data processing unit 206 for the purpose of monitoring, reporting, and verification, for example, as illustrated in FIG. 5 below. Although only one LIBS device is shown in the example system 200 of FIG. 2A, it is possible that more LIBS devices and/or other units/components may be included in a LIBS-based data system.|[0037] In some embodiments, at least a portion of the data processing unit 206 is part of a computer system (described below in FIG. 7) that is communicatively coupled to LIBS device 204. In other embodiments, at least a portion of the data processing unit 206 may be integrated into LIBS device 204. For example, data processing unit 206 may reside on a standalone computer system to perform advanced compositional analysis based on real-time sample analysis from data acquisition & analysis component 260 of LIBS device 204 (described below in FIG. 2B). Data processing unit 206 together with data acquisition & analysis component 260 form a data analysis subsystem that is responsible for various types of data processing, evaluation, calculation, etc, as described in the present disclosure. When LIBS device 204 is attached to or mounted on a motor instrument (e.g., vehicle, drone), the data analysis subsystem may be integrated into data acquisition onboard the motor instrument for real-time data acquisition and analysis. In some embodiments, at least a portion of the sample handling unit 202 may also be part of an external computer system and/or an integrated part of LIBS device 204. For example, sample handling unit 202 may be designed to use motorized stages or robots to move a sample in a controlled manner and thus is included in or attached to LIBS device 204 for precise sample positioning.|LIBS Device|[0038] LIBS is a rapid chemical analysis technology that uses a short laser pulse to create a micro-plasma on the sample surface. LIBS can be used to detect the presence of various elements in a sample based on directing a high-power emission from a laser onto the sample to form a plasma. The plasma is then analyzed spectroscopically to determine the composition of the sample. The LIBS is often used with a soil penetrating probe to detect heavy metal contamination in soil due to its high sensitivity and sample-free preparation. The LIBS analytical technique offers some other compelling advantages such as fast measurement time (e.g., a few seconds for a single spot analysis), broad elemental coverage (e.g., including, but not limited to, lighter elements such as H, Be, Li, C, N, O, Na, and Mg), versatile sampling protocols that include fast raster of the sample surface and depth profiling, etc.|[0039] The present disclosure proposes new LIBS device(s) used in the MRV process for ERW. In some embodiments, the new LIBS device is a single multi-purpose optical device. In other embodiments, the new LIBS device may include one or more optical devices. Each device can be designed for a single purpose or multiple purposes. The LIBS devices may have various physical components and/or configurations.|[0040] FIG. 2B illustrates an overall block diagram of an exemplary LIBS device 204, which includes some key components such as optical source 254, focusing and light collection optics 256, detector 258, and data acquisition & analysis component 260. These components are depicted merely for illustration, and other components (more or less) may be included in LIBS device 204. For example, sample probe 252 may be part of the LIBS device 204. In some embodiments, LIBS device 204 may use a sample probe 252 (e.g., a soil penetrating probe) to take a sample from a target area that is strategically identified (e.g., on managed land). In response, optical source 254 (e.g., a laser) may generate a high-energy light pulse that is directed onto the sample, and focusing and light collection optics 256 (e.g., lens, mirrors) may focus the light pulse to a specific point on the sample, thereby creating a plasma plume. The focusing and light collection optics 256 may also capture/collect the light pulse/beam to avoid light interference. The collected light pulse is then passed through detector 258 (e.g., spectrometer) to obtain sample measurements (e.g., spectral data). For example, detector 258 may disperse the light pulse into individual wavelengths, determine the intensity of light at each wavelength (e.g., using a charge-coupled device (CCD) or photo-multiplier tube (PMT)), and generate a spectrum that is characteristic of specific elements in the sample.|[0041] Data acquisition & analysis component 260 may include computing hardware such as a central processing unit, memory, and storage, as described in the computer system of FIG. 7. Data acquisition & analysis component 260 is configured to receive the measurement data from detector 258 and perform the elemental composition analysis on the measurement data. In some embodiments, LIBS device 204 may also communicate with an alternative or additional data processing unit (e.g., 206) to perform LIBS analysis and any other elemental identification and quantification analyses. Based on the analysis, a result is generated in 262. For example, the result may be a report or graphical output showing the elemental composition of the sample. Various types of measurements and analyses may be conducted by the data analysis subsystem including data acquisition & analysis component 260 and data processing unit 206, which will be further described below with reference to FIGS. 3-6.|[0042] The present system may deploy one or more improved LIBS devices to implement the disclosed functionalities. For example, the improved LIBS device (e.g., 204) may be equipped, attached, or associated with an autofocusing component to enable consistent, in-focus measurements of samples without moving other optical components. The autofocusing component may be included as a part of a suitable optical assembly that is hand-held, attached to a mobile vehicle, or integrated with a positioning system (e.g., robotic arm, boom, leg, conveyor belt), etc. Using the autofocusing component, spectroscopy measurements can be automatically focused based on a focal length of its optics relative to the target sample. Instead of using certain mechanisms (e.g., mechanical actuators) to change the position of the optical component(s), in some embodiments, the autofocusing component may include a shape changing lens (e.g., variable focus lens) to allow continuous tuning of a focal length and working distance of the autofocusing component relative to a target sample.|Data Acquisition and Evaluation Using LIBS Device|[0043] As discussed above, components 252, 254, 256, 258, and/or 260 of LIBS device 204 may work together with other units of data system 200 to acquire sample data and provide insights about the elemental composition of a sample (e.g., soil sample). In the illustrated embodiment of FIG. 3, one or more LIBS devices 204 may be used to determine weathering status 304, evaluate specific soil contents/elements 306, calculate heavy metal concentration 308, evaluate metal ratios in soils 310, and/or measure soil organic carbon 312. In some embodiments, one or more LIBS devices 200 may also be used to measure and analyze the compositional characteristics of soils, the biological composition of plant and seed matter, and the elemental composition of rock samples.|[0044] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304. In some embodiments, a LIBS-based device may be employed to assess the composition of lighter cations relative to heavier cations in applied rock dust. This composition analysis may be used in determining the weathering status of the rock dust application on agricultural fields, pasture lands, or any other natural environments. Thus, an approach is obtained, for determining the loss of rock dust due to enhanced rock weathering (ERW) for the purpose of monitoring, reporting, and verification (MRV) to create carbon credits.|[0045] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil. This is the estimation of nutrient requirements, factoring in additional nutrients provided by rock dust application. The use of LIBS devices in elemental composition analysis can reduce farmers' burden to apply fertilizers (i.e., NPK nitrogen-phosphorus-potassium) while conducting ERW projects. LIBS allows the quantification of these additional bioavailable nutrients, which become active in the soil column with the breakdown of the rock minerals (e.g., being modified through chemical, physical, or biological interactions with rocks and minerals).|[0046] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW. These elements may include metals such as lead (Pb), mercury (Hg), nickel (ni), etc., and can be found in pesticides, fertilizers, or untreated sewage sludge introduced into the soil. The heavy metal may accumulate in the environment to pose serious health and ecological risks. The disclosed LIBS device may provide insights into the safety considerations of cultivating various crops, for example, providing insights into phytoremediation such as using sunflowers to remove Strontium, which is poisonous metal to most other livings. According to US Environmental Protection Agency (EPA) standards, the bio-availability of metals and dissolved aqueous metals will be needed for calculating heavy metal concentrations.|[0047] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating key metal ratios in soils for ERW 310. In some embodiments, critical metal ratios in soils are assessed using LIBS technology before the implementation of ERW (i.e., before the rock dust application for enhanced weathering). This process can be outlined as follows:| - i. Sample Collection: soil samples are collected from the target area where ERW is planned. These samples represent the current soil composition in the region;| - ii. LIBS Analysis: the collected soil samples are subjected to LIBS analysis. The LIBS device measures the elemental composition of the soil, providing baseline data on the concentrations of various metals being present;| - iii. Trace metal ratios and potential pulverized rock dust field amendments may then be evaluated together to determine if the rock dust is appropriate for application to the field; and | - a. Evaluate environmental concerns,| - b. Evaluate the potential for signal strength in measurements: measuring key metal ratios for MRV process.| - iv. Key Metal Ratios: specific metal ratios of interest, which are known to influence the effectiveness of ERW, are calculated based on the LIBS data. These key metal ratios often include ratios such as calcium to magnesium (Ca/Mg), calcium to potassium (Ca/K), or calcium to sodium (Ca/Na), among others.|[0054] In some embodiments, the calculated key metal ratios are evaluated to determine the suitability of the soil for ERW. An ideal balance of these ratios is typically necessary for optimal carbon capture and weathering outcomes. The assessment results may guide decisions regarding the need for rock dust application and the specific rock dust type required to achieve the desired metal ratios for effective ERW.|[0055] By employing LIBS technology for the evaluation of key metal ratios in soils before rock dust application for enhanced weathering, informed decision-making can be used to ensure that the chosen ERW strategy is tailored to the specific soil composition of the target area. This optimization may also contribute to efficient carbon dioxide removal and MRV.|[0056] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for measuring soil organic carbon 312. A LIBS device can be used to measure soil organic carbon (SOC) levels. The SOC level represents the amount of carbon stored in the form of organic compounds in the soil, and SOC is critical to soil quality and carbon sequestration because it helps store carbon from the atmosphere and contributes to mitigating climate change. By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement. In some embodiments, soil organic carbon measurements may be approximated by the loss of material on ignition (LOI) (e.g., by measuring the weight loss of organic matter content after heating the sample to a high temperature).|LIBS Analysis|[0057] Numerous LIBS analyses may be conducted based on element measurements, calculation, and evaluation. In addition to in-depth soil analysis, when a LIBS device is used to measure the biological composition of plant and seed matter, the LIBS analysis can serve to validate the absence of potential metal accumulation resulting from enhanced weathering processes.|[0058] In some embodiments, a LIBS device may also be used for rock sample analysis, where the elemental composition of raw rock samples from rock quarries or in the field is analyzed. This LIBS analysis may be applied to determine an enhanced weathering potential and a total carbon dioxide removal (CDR) potential. The enhanced weathering potential is the amount of atmospheric carbon dioxide that can be removed and stored through the ERW process (e.g., manual application of rocks or minerals) over a specific period of time. This factor may vary depending on the type of rocks/minerals used in ERW, the surface area available for reaction, environmental conditions (e.g., precipitation, temperature), etc. The total CDR potential is the amount of carbon dioxide that can be removed from the atmosphere in the long term, which depends on the effectiveness of the ERW process.|[0059] In some embodiments, a spectral fluorescence device may be used in combination with LIBS analysis to create a dual system. This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status. In some embodiments, this approach may also be used to help refine soil organic carbon estimates outlined in 312 of FIG. 3. In general, the combination of LIBS and fluorescence may expand and strengthen the LIBS measurement and analysis, e.g., as discussed in FIG. 3.|Beneficial Features of LIBS Device and Analysis|[0060] FIG. 4 illustrates a block diagram 400 of exemplary features of LIBS devices and analysis used in the MRV process for ERW as described in the present system.|[0061] The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402. By aggregating soil samples from various locations within a field, the present system seeks to accurately determine the central compositional tendency and associated dispersion or variance in the soil's elemental composition. As compared to the current techniques, the utilization of pooled samples enables a more robust and representative analysis of the soil's overall composition, contributing to a more precise assessment of soil quality and environmental conditions. The accurate measurement of pooled samples is particularly important to soil fertility assessment, soil quality monitoring, and precision agriculture.|[0062] The present system provides geolocated zone-based soil sampling for target characteristic assessment, as shown in 404. In some embodiments, the present system allows the collection of soil samples from specific geolocated zones within a field. By strategically pooling samples from these distinct zones, the analysis can yield precise data regarding the central tendency and variance of the target characteristic within each zone. This geolocated zone-based sampling approach offers a granular understanding of the spatial heterogeneity, distribution, and variability of the target characteristic, thereby enabling informed decision-making for soil management and ERW applications. Potential future obstacles with a MRV process based on soil heterogeneity may also be addressed by examining measurements at this juncture. In some embodiments, zones may be determined based on soil type, gridded areas, etc. A zone may also be small, predefined regions that include, but are not limited to, a circular region with a predefined radius or a square area with a predefined side length.|[0063] The LIBS device of the present system can be used in rock sample analysis to determine enhanced weathering potential and total carbon dioxide removal (CDR) potential. In particular, the present system may evaluate the carbon dioxide potential of alkaline silicate minerals, as shown in 406. The present system can assess the carbon dioxide potential of alkaline silicate minerals including, but not limited to, basalt, olivine, and wollastonite. These minerals are known for their capacity to sequester carbon dioxide through enhanced weathering processes. In some embodiments, the present system may utilize a LIBS device to analyze the elemental composition of these minerals and determine their specific potential for CDR. By accurately quantifying the CDR potential of alkaline silicate minerals, the present system gains valuable insights into the efficacy of a CDR solution.|[0064] The present system allows systematic preparation of pressed-pelletized subsamples derived from pooled soil samples, as shown in 408. By compressing and pelletizing soil material from each pooled sample, the present system may create a consistent and standardized substrate for LIBS analysis. This process can minimize variations in sample presentation, ensuring reliable and reproducible results during LIBS analysis. This process further streamlines the handling of samples, allowing for an efficient assessment of the central compositional tendency and variance of the target characteristics within the soil, and ultimately enhancing the accuracy of soil quality and environmental assessments.|[0065] The present system further allows grid-based or rastered LIBS sampling for in-depth soil core analysis, as shown in 410. In some embodiments, the present system may conduct grid-based or rastered analyses of the pelletized subsamples, where the LIBS device systematically scans and analyzes discrete regions or points on the pellet surface in a structured grid or raster pattern. This approach enables a comprehensive examination of the intersample heterogeneity (or microheterogeneity) of soil characteristics and the distribution of elemental composition within the subsamples.|[0066] Through this analysis, the present system may achieve a high-resolution understanding of the central compositional tendency and variance of the target characteristics in the soil, and the detailed information may provide invaluable insights into the spatial variability of soil properties, thereby enhancing precision in soil quality assessment and MRV for CDR applications.|[0067] Using rasterized or gridded LIBS sampling can also systematically measure the elemental composition of intact soil cores at various depths. By taking measurements in a prescribed structured grid or raster pattern for LIBS analysis along the length of an intact soil core, the present approach enables precise characterization of the compositional variations with depth. This is particularly beneficial for understanding how soil properties change at different depths within the core, offering crucial insights into subsurface composition and environmental conditions. The present system seeks to assess soil heterogeneity and geological attributes with depth, contributing to informed decisions in ERW applications and MRV techniques.|Device Characteristics and Deployment|[0068] The present system supports specific device characteristics and deployment that are beneficial to the MRV process for ERW. In some embodiments, the present system supports handheld and miniaturized LIBS devices for soil sampling, field-based depth-integrated soil profiling with LIBS and soil auger, and in-field deployment of LIBS technology on motor vehicles, etc.|[0069] The LIBS device described herein can be a handheld device that is portable, easy to operate, and suitable for rapid data acquisition. This handheld device is particularly useful in patchwork small-holder farms (e.g., rice paddies). It is engineered to provide a simplified user interface while maintaining the analytical accuracy and precision required for soil and environmental analysis. Any instantiation of the LIBS device may contain fewer optical sensors than the original, making the device more affordable and lighter. As a result, this LIBS device is adaptive for use in rural, remote, and economically disadvantaged communities. In addition, the miniaturized form of the device enables the present system to perform real-time, in-situ analyses, contributing to timelier and data-driven decision-making processes in agriculture, geology, and environmental science.|[0070] The present system also allows a LIBS device to be combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic. A soil auger is employed to collect soil samples at various depths within the field. These samples are representative of the soil composition at specific depth intervals.|[0071] After and/or during the auguring process, the present system performs LIBS analysis on the collected soil samples. A LIBS device can rapidly and accurately measure the elemental composition of the soil samples, including the concentration of the target characteristic of interest. The present system may then integrate the LIBS data obtained from each depth interval to construct a depth-integrated soil profile of the target characteristic. This profile provides a comprehensive understanding of how the target characteristic varies with depth within the soil.|[0072] A LIBS device/instrument can be deployed in different ways. In some embodiments, the present system supports in-field deployment of LIBS technology on motor vehicles. LIBS is integrated into motor vehicles, such as tractors or other agricultural machinery, for in-field deployment. The present system seamlessly integrates LIBS instrumentation into the design of motor vehicles used for field operations, such as tractors.|[0073] The LIBS device can be securely mounted, ensuring stability during vehicle movement. The LIBS device may operate in real time as the motor vehicle traverses the field. The LIBS device continuously analyzes the soil or other target materials as the vehicle moves, providing instant elemental composition data. The present system may collect LIBS-generated data and integrate the data into a data acquisition (DAQ) onboard the vehicle, allowing for real-time decision-making based on soil or material composition. A vehicle operator can use the LIBS data to make immediate adjustments to field operations for any ERW-related purpose, such as varying fertilizer application rates or adjusting rock dust application rates based on the in-field analysis. The present system may log the LIBS data, providing a detailed record of the soil or material composition across the field for subsequent analysis and optimization.|[0074] In some embodiments, the present system may support other deployment methods. For example, one or more LIBS devices may be integrated into drones, underwater vehicles/amphibious, or other mobil instruments.|Data Analysis and Modeling|[0075] FIG. 5 illustrates a block diagram 500 of exemplary features of data analysis and modeling used in the present system. As depicted in FIG. 5, the data analysis and modeling 502 of the present system may be featured with various analytical tools such as multivariate distribution modeling for cation covariance analysis 504, empirical modeling for weathering prediction and carbon credit creation 506, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data 508, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS 510, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV 512. In some embodiments, these data analyses and modeling may be performed at least by data processing unit 206 in combination with data acquisition & analysis component 260 as shown in FIGS. 2A and 2B (i.e., data analysis subsystem).|[0076] The present system provides multivariate distribution modeling for cation covariance analysis, as shown in 504. In some embodiments, the LIBS data can be leveraged for analyzing and modeling the covariance relationships among key cations in soil including, but not limited to, titanium, calcium, sodium, magnesium, potassium, phosphorous, and nitrogen. In some embodiments, the present system entails fitting multivariate normal or non-normal distributions to the data obtained through LIBS measurements.|[0077] Multivariate distribution fitting allows for the comprehensive assessment of the covariance and correlations between key cations in soil. It provides valuable insights into the simultaneous variations and relationships among these elements, contributing to a deep understanding of soil composition and baseline information required for MRV. The present system uses LIBS to provide dense and rapid enough data to find systematic variances in soil heterogeneity within any given field, pasture, agricultural setting, or any other natural setting.|[0078] In some embodiments, the present system may apply the quantitative elemental analysis approach as described in Sobron, titled “non-linear methods for quantitative elemental analysis and mineral classification using laser-induced breakdown spectroscopy (LIBS),” U.S. patent application Ser. No. 15/998,391, which is hereby incorporated by reference in its entirety.|[0079] In some embodiments, the present system supports empirical modeling for weathering prediction and carbon credit creation, as shown in 406. That is, data collected in the present system can be leveraged to develop an empirically driven model for predicting the weathering of rock dust applied to fields and providing suggestions and instructions for subsequent ERW implementation.|[0080] The empirical model may help the monitoring, reporting, and verification (MRV) process, which aims at quantifying the carbon capture potential resulting from enhanced weathering practices. By using dense, LIBS-generated data to create a predictive model, it becomes possible to monitor and report on the efficiency of carbon capture using regression-based and/or machine-learning methods. As a result, the time between data collection and sales for creating carbon credits may be reduced. The empirically driven model therefore facilitates accurate and data-driven MRV processes while incentivizing an easy switch to practices where carbon credits may be created through ERW. For example, when structure a predictive model, the present system may use mineral type, application rate, surface area of mineral, climate data, and environmental carbon dioxide concentration as input parameters of the model. The present system may calculate the weathering rate based on the environmental conditions and mineral properties, calculate the sequestration of carbon dioxide, and use weathering rate equations to predict how much carbon dioxide may be captured within a specific area over a specific timeframe. The present system may also calculate the total carbon dioxide removal rate to estimate global or regional carbon dioxide sequestration potential.|[0081] To ensure accuracy and precision, in some embodiments, the present system may calibrate the LIBS device using high-precision measurements obtained from ICP-MS, as shown in 508.|[0082] ICP-MS represents a well-established and highly accurate analytical technique, known for its exceptional precision in measuring elemental composition. By calibrating the LIBS device against ICP-MS data, the present system may establish a robust and reliable calibration framework. This calibration method may serve to validate and fine-tune the LIBS measurements, ensuring accuracy and traceability to a gold standard in elemental analysis.|[0083] The integration of ICP-MS calibration in the present system enhances the trustworthiness and consistency of LIBS measurements, and the enhanced measurements may be suitable for a wide range of ERW applications for MRV. This calibration approach boosts the credibility of LIBS technology in scientific research and regulatory compliance (e.g., metals contamination according to EPA standards).|[0084] The present system supports the construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, as shown in 510. In some embodiments, the present system may use known mixtures of soil and rock dust to create calibration curves. With a soil sample and rock dust sample that have already been characterized via ICP-MS or other analytical techniques, the present system can obtain known mixtures such that the rock dust comprises a known percentage of the weight of a newly created sample. By testing many mixed samples using LIBS with an array of rock dust ranging from 0 to 100% weight by mass, the present system can determine a series of calibration curves. These curves may fit the compositional characteristics of a particular soil type-rock dust combination. The present system may then store the data for soil type-rock dust combinations, creating a large database of possible LIBS spectral signals for a range of possible compositional arrays. With a sufficiently large database, the present system can apply one or more regression-based, machine-learning-based tools, and principal component analysis to select the most optimal calibration curve for new measurement(s).|[0085] Here, the present system aims to strengthen the credibility of carbon credit generation. In some embodiments, the present system may use the misfit of measurements to known calibration curves to quantify measurement uncertainty, so that carbon credit sales effectively incorporate potential variations in carbon capture into pricing structures.|[0086] In some embodiments, the present system supports collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV, as shown in 512. In other words, ICP-MS and LIBS are used collaboratively to spot-check and validate the empirically driven model developed for CDR MRV. This process ensures that the model accurately reflects the carbon capture and sequestration processes in real-world applications, enhancing the reliability of carbon credit generation. The present system may also use the same collaborative framework to generate uncertainty models when upscaling the sample area for MRV. To upscale the sample area for MRV, test plots are used to make projections for larger fields, and/or several fields are used to project CDR for a region, etc. By systematically assessing variations and uncertainties using ICP-MS and LIBS data, these models provide insights into the potential variability in carbon capture estimates as the sample area is expanded. This information is essential for accurately quantifying carbon credits and assuaging buyers' concerns about the quality of carbon credits. The information is also crucial to assess the quality of MRV.|[0087] The present system aims to strengthen the credibility of carbon credit generation and improve informed decision-making in ERW-related land management. By integrating uncertainty modeling, the present system enhances its ability to account for variations in carbon capture and carbon dioxide removal potential and provides a comprehensive assessment of carbon dioxide removal efforts. The present system may enhance the credibility of carbon credit generation while providing transparency and accountability in environmental initiatives.|Flowchart|[0088] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments. Method 600 may be implemented using a LIBS-based data system 200, as shown in FIGS. 2A and 2B. A spectroscopy device (e.g., LIBS device 204) is used to obtain measurements from a target sample. At step 602, the spectroscopy device (e.g., using optical source 254) emits one or more optical signals directed to a target collected from a target area (e.g., managed field or other agricultural settings). At step 604, the spectroscopy device (e.g., using detector 258) determines spectral measurements of the optical signals collected from the target. The target can be a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified (e.g., by sample handing unit 202) from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered LIBS sampling.|[0089] As shown in FIGS. 2A and 2B, a data analysis subsystem (e.g., including data processing unit 206 and data acquisition & analysis component 260) is communicatively coupled to the spectroscopy device (e.g., LIBS device 204). At step 606, the data analysis subsystem is configured to convert the spectral measurements to data indicating compositional characteristics of the target, which includes at least one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. For example, to determine the weathering status, loss of rock dust may be determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering.|[0090] The data analysis subsystem is then configured to analyze the data indicating compositional characteristics of the target using a plurality of analytical tools at step 608, and provide assessment on carbon dioxide removal and insights on enhanced rock weathering at step 610. In some embodiments, to analyze the compositional data, the data analysis subsystem uses various analytical tools to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision ICP-MS data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS, etc. To provide the assessment, the data analysis subsystem may also calculate one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.|Computer Implementation|[0091] In some examples, some or all of the processing described above can be carried out on a personal computing device, on one or more centralized computing devices, or via cloud-based processing by one or more servers. Some types of processing can occur on one device and other types of processing can occur on another device. Some or all of the data described above can be stored on a personal computing device, in data storage hosted on one or more centralized computing devices, and/or via cloud-based storage. Some data can be stored in one location and other data can be stored in another location. In some examples, quantum computing can be used, and/or functional programming languages can be used. Electrical memory, such as flash-based memory, can be used.|[0092] FIG. 7 is a block diagram of an example computer system 700 that may be used in implementing the technology described herein. General-purpose computers, network appliances, mobile devices, or other electronic systems may also include at least portions of the system 700. The system 700 includes a processor 710, a memory 720, a storage device 730, and an input/output device 740. Each of the components 710, 720, 730, and 740 may be interconnected, for example, using a system bus 750. The processor 710 is capable of processing instructions for execution within the system 700. In some implementations, the processor 710 is single-threaded. In some implementations, the processor 710 is a multi-threaded processor. The processor 710 is capable of processing instructions stored in the memory 720 or on the storage device 730.|[0093] Memory 720 stores information within the system 700. In some implementations, the memory 720 is a non-transitory computer-readable medium. In some implementations, the memory 720 is a volatile memory unit. In some implementations, the memory 720 is a non-volatile memory unit.|[0094] The storage device 730 is capable of providing mass storage for the system 700. In some implementations, the storage device 730 is a non-transitory computer-readable medium. In various implementations, the storage device 730 may include, for example, a hard disk device, an optical disk device, a solid-state drive, a flash drive, or some other large-capacity storage device. For example, the storage device may store long-term data (e.g., database data, file system data, etc.). The input/output device 740 provides input/output operations for the system 700. In some implementations, the input/output device 740 may include one or more network interface devices, e.g., an Ethernet card, a serial communication device, e.g., an RS-232 port, and/or a wireless interface device, e.g., an 802.11 card, a 3G wireless modem, or a 4G wireless modem. In some implementations, the input/output device may include driver devices configured to receive input data and send output data to other input/output devices, e.g., keyboard, printer, and display devices 760. In some examples, mobile computing devices, mobile communication devices, and other devices may be used.|[0095] In some implementations, at least a portion of the approaches described above may be realized by instructions that upon execution cause one or more processing devices to carry out the processes and functions described above. Such instructions may include, for example, interpreted instructions such as script instructions, executable code, or other instructions stored in a non-transitory computer-readable medium. The storage device 730 may be implemented in a distributed way over a network, such as a server farm or a set of widely distributed servers, or may be implemented in a single computing device.|[0096] Although an example processing system has been described in FIG. 7, embodiments of the subject matter, functional operations, and processes described in this specification can be implemented in other types of digital electronic circuitry, in tangibly embodied computer software or firmware, in computer hardware, including the structures disclosed in this specification and their structural equivalents, or in combinations of one or more of them. Embodiments of the subject matter described in this specification can be implemented as one or more computer programs, i.e., one or more modules of computer program instructions encoded on a tangible nonvolatile program carrier for execution by, or to control the operation of, data processing apparatus. Alternatively or in addition, the program instructions can be encoded on an artificially generated propagated signal, e.g., a machine-generated electrical, optical, or electromagnetic signal that is generated to encode information for transmission to a suitable receiver apparatus for execution by a data processing apparatus. The computer storage medium can be a machine-readable storage device, a machine-readable storage substrate, a random or serial access memory device, or a combination of one or more of them.|[0097] The term “system” may encompass all kinds of apparatus, devices, and machines for processing data, including by way of example a programmable processor, a computer, or multiple processors or computers. A processing system may include special-purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit). A processing system may include, in addition to hardware, code that creates an execution environment for the computer program in question, e.g., code that constitutes processor firmware, a protocol stack, a database management system, an operating system, or a combination of one or more of them.|[0098] A computer program (which may also be referred to or described as a program, software, a software application, a module, a software module, a script, or code) can be written in any form of programming language, including compiled or interpreted languages, or declarative or procedural languages, and it can be deployed in any form, including as a standalone program or as a module, component, subroutine, or other unit suitable for use in a computing environment. A computer program may, but need not, correspond to a file in a file system. A program can be stored in a portion of a file that holds other programs or data (e.g., one or more scripts stored in a markup language document), in a single file dedicated to the program in question, or in multiple coordinated files (e.g., files that store one or more modules, sub programs, or portions of code). A computer program can be deployed to be executed on one computer or on multiple computers that are located at one site or distributed across multiple sites and interconnected by a communication network.|[0099] The processes and logic flows described in this specification can be performed by one or more programmable computers executing one or more computer programs to perform functions by operating on input data and generating output. The processes and logic flows can also be performed by, and apparatus can also be implemented as, special purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit).|[0100] Computers suitable for the execution of a computer program can include, by way of example, general or special purpose microprocessors or both, or any other kind of central processing unit. Generally, a central processing unit will receive instructions and data from a read-only memory, a random access memory, or both. A computer generally includes a central processing unit for performing or executing instructions and one or more memory devices for storing instructions and data. Generally, a computer will also include, or be operatively coupled to receive data from or transfer data to, or both, one or more mass storage devices for storing data, e.g., magnetic, magneto-optical disks, or optical disks. However, a computer need not have such devices. Moreover, a computer can be embedded in another device, e.g., a mobile telephone, a personal digital assistant (PDA), a mobile audio or video player, a game console, a Global Positioning System (GPS) receiver, or a portable storage device (e.g., a universal serial bus (USB) flash drive), to name just a few.|[0101] Computer-readable media suitable for storing computer program instructions and data include all forms of non-volatile memory, media, and memory devices, including by way of example semiconductor memory devices, e.g., EPROM, EEPROM, and flash memory devices; magnetic disks, e.g., internal hard disks or removable disks; magneto-optical disks; and CD-ROM and DVD-ROM disks. The processor and the memory can be supplemented by, or incorporated in special-purpose logic circuitry.|[0102] To provide for interaction with a user, embodiments of the subject matter described in this specification can be implemented on a computer having a display device, e.g., a CRT (cathode ray tube) or LCD (liquid crystal display) monitor, for displaying information to the user and a keyboard and a pointing device, e.g., a mouse or a trackball, by which the user can provide input to the computer. Other kinds of devices can be used to provide for interaction with a user as well; for example, feedback provided to the user can be any form of sensory feedback, e.g., visual feedback, auditory feedback, or tactile feedback; and input from the user can be received in any form, including acoustic, speech, or tactile input. In addition, a computer can interact with a user by sending documents to and receiving documents from a device that is used by the user; for example, by sending web pages to a web browser on a user's user device in response to requests received from the web browser.|[0103] Embodiments of the subject matter described in this specification can be implemented in a computing system that includes a back-end component, e.g., as a data server, or that includes a middleware component, e.g., an application server, or that includes a front-end component, e.g., a client computer having a graphical user interface or a Web browser through which a user can interact with an implementation of the subject matter described in this specification, or any combination of one or more such back end, middleware, or front end components. The components of the system can be interconnected by any form or medium of digital data communication, e.g., a communication network. Examples of communication networks include a local area network (“LAN”) and a wide area network (“WAN”), e.g., the Internet.|[0104] The computing system can include clients and servers. A client and server are generally remote from each other and typically interact through a communication network. The relationship between client and server arises by virtue of computer programs running on the respective computers and having a client-server relationship with each other.|[0105] While this specification contains many specific implementation details, these should not be construed as limitations on the scope of what may be claimed, but rather as descriptions of features that may be specific to particular embodiments. Certain features that are described in this specification in the context of separate embodiments can also be implemented in combination in a single embodiment. Conversely, various features that are described in the context of a single embodiment can also be implemented in multiple embodiments separately or in any suitable sub-combination. Moreover, although features may be described above as acting in certain combinations and even initially claimed as such, one or more features from a claimed combination can in some cases be excised from the combination, and the claimed combination may be directed to a sub-combination or variation of a sub-combination.|[0106] Similarly, while operations are depicted in the drawings in a particular order, this should not be understood as requiring that such operations be performed in the particular order shown or in sequential order, or that all illustrated operations be performed, to achieve desirable results. In certain circumstances, multitasking and parallel processing may be advantageous. Moreover, the separation of various system components in the embodiments described above should not be understood as requiring such separation in all embodiments, and it should be understood that the described program components and systems can generally be integrated together in a single software product or packaged into multiple software products.|[0107] Particular embodiments of the subject matter have been described. Other embodiments are within the scope of the following claims. For example, the actions recited in the claims can be performed in a different order and still achieve desirable results. As one example, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In certain implementations, multitasking and parallel processing may be advantageous. Other steps or stages may be provided, or steps or stages may be eliminated, from the described processes. Accordingly, other implementations are within the scope of the following claims.|Terminology|[0108] The phraseology and terminology used herein are for the purpose of description and should not be regarded as limiting.|[0109] The term “approximately”, the phrase “approximately equal to”, and other similar phrases, as used in the specification and the claims (e.g., “X has a value of approximately Y” or “X is approximately equal to Y”), should be understood to mean that one value (X) is within a predetermined range of another value (Y). The predetermined range may be plus or minus 20%, 10%, 5%, 3%, 1%, 0.1%, or less than 0.1%, unless otherwise indicated.|[0110] The indefinite articles “a” and “an,” as used in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.” The phrase “and/or,” as used in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Multiple elements listed with “and/or” should be construed in the same fashion, i.e., “one or more” of the elements so conjoined. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, a reference to “A and/or B”, when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A only (optionally including elements other than B); in another embodiment, to B only (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.|[0111] As used in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law.|[0112] As used in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.|[0113] The use of “including,” “comprising,” “having,” “containing,” “involving,” and variations thereof, is meant to encompass the items listed thereafter and additional items.|[0114] Use of ordinal terms such as “first,” “second,” “third,” etc., in the claims to modify a claim element does not by itself connote any priority, precedence, or order of one claim element over another or the temporal order in which acts of a method are performed. Ordinal terms are used merely as labels to distinguish one claim element having a certain name from another element having a same name (but for use of the ordinal term), to distinguish the claim elements.|[0115] Each numerical value presented herein, for example, in a table, a chart, or a graph, is contemplated to represent a minimum value or a maximum value in a range for a corresponding parameter. Accordingly, when added to the claims, the numerical value provides express support for claiming the range, which may lie above or below the numerical value, in accordance with the teachings herein. Absent inclusion in the claims, each numerical value presented herein is not to be considered limiting in any regard.|[0116] The terms and expressions employed herein are used as terms and expressions of description and not of limitation, and there is no intention, in the use of such terms and expressions, of excluding any equivalents of the features shown and described or portions thereof. In addition, having described certain embodiments of the invention, it will be apparent to those of ordinary skill in the art that other embodiments incorporating the concepts disclosed herein may be used without departing from the spirit and scope of the invention. The features and functions of the various embodiments may be arranged in various combinations and permutations, and all are considered to be within the scope of the disclosed invention. Accordingly, the described embodiments are to be considered in all respects as only illustrative and not restrictive. Furthermore, the configurations, materials, and dimensions described herein are intended as illustrative and in no way limiting. Similarly, although physical explanations have been provided for explanatory purposes, there is no intent to be bound by any particular theory or mechanism, or to limit the claims in accordance therewith. Family Number|(114579754)|114579754|Abstract|(US20250164404 A1)|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.|CPC codes|(US20250164404 A1)|G01N-021/71/8|G01N-033/24/1|G01N-033/245|G01N-033/24|G01N-2201/0216|G01N-2201/0221|G01N-2201/06113|G01N-2201/12746|IPC codes|(US20250164404 A1)|G01N-021/71|G01N-033/24|Title|(US20250164404 A1)|System and method for enhanced rock weathering monitoring, reporting, and verification| Analysis of biological materials G01N-021/71/8|G01N-033/24|G01N-033/24/1|G01N-033/245|G01N-2201/0216|G01N-2201/0221|G01N-2201/06113|G01N-2201/12746 G01N-021/71/8|G01N-033/24|G01N-033/24/1|G01N-033/245|G01N-2201/0216|G01N-2201/0221|G01N-2201/06113|G01N-2201/12746 G01N-021/71|G01N-033/24 G01N-021/71|G01N-033/24 PENDING (US20250164404)|PENDING ALIVE (US20250164404)|ALIVE (US20250164404)|LEGAL DETAILS FOR US20250164404|Actual or expected expiration date=2044-11-20|Legal state=ALIVE|Status=PENDING|Event publication date=2024-11-20|Event code=US/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=US US18954208|Application date=2024-11-20|Standardized application number=2024US-18954208|Event publication date=2024-11-20|Event code=US/EXMR|Event group=Administrative notifications|USPTO Examiner Name|PRIMARY EXAMINER:DOUMBIA, MOHAMED|Event publication date=2024-11-20|Event code=US/DK|Event group=Examination events|Attorney Docket Number|Docket Nbr: IMS-002US|Event publication date=2024-11-20|Event code=US/CUST|Event group=Examination events|Attorney/Agent Customer Number|Customer Nbr: 162143|Event publication date=2024-11-20|Event code=US/SMALL|Event group=Administrative notifications|Appl Has Filed a Verified Statement of Micro to Small Entity Status|Business Entity Status: Small|Event publication date=2024-11-20|Event code=US/AIA|Event group=Administrative notifications|First Inventor File Indicated:|AIA=Yes|Event publication date=2024-11-20|Event code=US/ART|Event group=Administrative notifications|USPTO Art Group|ART=2877|Event publication date=2024-11-20|Event code=US/IDS|Event group=Examination events OAI|Information Disclosure Statement Filed|Event publication date=2024-11-20|Event code=US/ENT|Event group=Administrative notifications|Entity Status Set to Undiscounted|Event publication date=2024-11-20|Event code=US/PTARDY|Event indicator=Pos|Event group=Examination events|Patent Term Adjustment - Ready for Examination|Event publication date=2024-11-26|Event code=US/SMALL|Event group=Administrative notifications|Appl Has Filed a Verified Statement of Micro to Small Entity Status|Event publication date=2024-11-29|Event code=US/POAC|Event group=Change of name or address|Change in Power of Attorney (May Include Associate POA)|Event publication date=2024-11-29|Event code=US/APPFILEREC|Event group=Administrative notifications OAO|Filing Receipt|Event publication date=2024-12-27|Event code=US/DKNC|Event indicator=Pos|Event group=Examination events|Docketed New Case - Ready for Examination|Event publication date=2024-12-27|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner|Event publication date=2025-05-22|Event code=US/A1|Event group=Examination events|Application published|Publication country=US|Publication number=US20250164404|Publication stage code=A1|Publication date=2025-05-22|Standardized publication number=US20250164404|Event publication date=2025-05-22|Event code=US/PGPUBN|Event indicator=Pos|Event group=Examination events OAO|PG-Pub Issue Notification|Event publication date=2026-03-22|Event code=US/DOCK|Event indicator=Pos|Event group=Examination events|Case Docketed to Examiner (US20250164404)|US https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcOL9D3zefy0h3ePXCJGwxO7JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022751788&ekey=2410&xpn=US20250164404&kind=A1 https://data.uspto.gov/patent-file-wrapper/search/details/18954208/application-data https://permalink.orbit.com/RenderStaticFirstPage?XPN=YH%252BWdJIGbNl11gTCkuP4xcRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT US (US20250164404)|US (US20250164404)|NAME=Impossible Sensing LLC , CITY=St. Louis , STATE=MO , COUNTRY=US NAME=Mati Carbon PBC , CITY=Wilmington , STATE=DE , COUNTRY=US (US20250164404)|US; US; US (US20250164404)|NAME=Sobron Pablo, CITY=St. Louis, STATE=MO , COUNTRY=US |NAME=Jordan Jacob S., CITY=St. Louis, STATE=MO , COUNTRY=US |NAME=Agarwal Shantanu, CITY=Houston, STATE=TX , COUNTRY=US 0 1 Titre: (US20250164404)|System and method for enhanced rock weathering monitoring, reporting, and verification Résumé: (US20250164404)|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering. 77 Abstract gpt-4o-mini uncertain The article discusses monitoring and verification of enhanced rock weathering, but does not explicitly detail the processes or technologies aimed at accelerating mineral alteration for CO₂ capture.
78 US63/118,677|US63/118,677P|US18/038,813|WOIB2021/061024 ECDI202346201|CL2023001495|WOIB2021/061024|HK62024088272|IN202317042083|CO2023007635|DO2023000105|AEP6001220/2023|ZA202305467|EP21897298|JP2023531576|AU2021389080|US18/038,813|VN1202303384|CR20230285|PE2023001728|TH20231002998|CN202180091927|KR10-2023-7020913|IL303119|SG11202303717V|BR112023010037|IDP00202304917|MX2023006141|CA3198500 ZA202305467|AEP6001220/2023|EP4251775|JP2023553314|IN202317042083|AU2021389080|HK40100255|US20240002973|JP2023553314|VN98973|CR20230285|CL2023001495|ECSP23046201|PE20231629|TH2301002998|EP4251775|CN116802326|DOP2023000105|KR10-2023-0110773|CO2023007635|IL303119|SG11202303717V|AU2021389080|BR112023010037|ID2023/04650|MX2023006141|BR112023010037|WO2022/113025|CA3198500|WO2022/113025 100294161 ECSP23046201 A 2023-10-31 [EC2346201]|CL2023001495 A1 2023-11-03 [CL202301495]|WO2022/113025 A3 2022-09-29 [WO2022113025]|WO2022/113025 A2 2022-06-02 [WO2022113025]|HK40100255 A 2024-04-26 [HK40100255]|IN202317042083 A 2024-08-02 [IN202317042083]|CO2023007635 A2 2023-07-21 [CO2023007635]|DOP2023000105 A 2023-08-31 [DO202300105]|AEP6001220/2023 A1 2024-12-17 [AE20236001220]|ZA202305467 B 2025-09-25 [ZA202305467]|EP4251775 A4 2024-12-11 [EP4251775]|EP4251775 A2 2023-10-04 [EP4251775]|JP2023553314 A5 2024-12-05 [JP2023553314]|JP2023553314 A 2023-12-21 [JP2023553314]|AU2021389080 A9 2024-06-27 [AU2021389080]|AU2021389080 A1 2023-06-22 [AU2021389080]|US20240002973 A1 2024-01-04 [US20240002973]|VN98973 A 2023-11-27 [VN--98973]|CR20230285 A 2023-11-06 [CR202300285]|PE20231629 A1 2023-10-11 [PE202301629]|TH2301002998 A 2023-10-09 [TH20230002998]|CN116802326 A 2023-09-22 [CN116802326]|KR10-2023-0110773 A 2023-07-25 [KR20230110773]|IL303119 A 2023-07-01 [IL-303119]|SG11202303717V A 2023-06-28 [SG11202303717V]|BR112023010037 A2 2023-06-20 [BR112023010037]|BR112023010037 A0 2023-05-30 [BR112023010037]|ID2023/04650 A 2023-06-08 [ID202304650]|MX2023006141 A 2023-06-06 [MX2023006141]|CA3198500 A1 2022-06-02 [CA3198500] 2020-11-26|2021-11-26 2023-06-20|2023-05-24|2021-11-26|2024-03-05|2023-06-23|2023-06-09|2023-05-25|2023-05-23|2023-05-19|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26|2021-11-26 2025-09-25|2024-12-17|2024-12-11|2024-12-05|2024-08-02|2024-06-27|2024-04-26|2024-01-04|2023-12-21|2023-11-27|2023-11-06|2023-11-03|2023-10-31|2023-10-11|2023-10-09|2023-10-04|2023-09-22|2023-08-31|2023-07-25|2023-07-21|2023-07-01|2023-06-28|2023-06-22|2023-06-20|2023-06-08|2023-06-06|2023-05-30|2022-09-29|2022-06-02|2022-06-02 |||||(ZA202305467)|2025-09-25||||||||||||||||||| (EP4251775)|2041-11-26|(US20240002973)|2041-11-26|(WO2022/113025)|2024-05-26|(JP2023553314)|2041-11-26|(CN116802326)|2041-11-26|(ZA202305467)|2041-11-26|(AEP6001220/2023)|2041-11-26|(IN202317042083)|2041-11-26|(AU2021389080)|2041-11-26|(HK40100255)|2041-11-26|(VN98973)|2041-11-26|(CR20230285)|2041-11-26|(CL2023001495)|2043-05-24|(ECSP23046201)|2043-06-20|(PE20231629)|2041-11-26|(TH2301002998)|2041-11-26|(DOP2023000105)|2041-11-26|(KR10-2023-0110773)|2041-11-26|(CO2023007635)|2041-11-26|(IL303119)|2041-11-26|(SG11202303717V)|2041-11-26|(BR112023010037)|2041-11-26|(ID2023/04650)|2041-11-26|(MX2023006141)|2041-11-26|(CA3198500)|2041-11-26 (EP4251775)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values (EP4251775)|Processes are provided in which successive steps of hydrometallurgical value extraction may be carried out using the products of carbon capture and an electrolytic reagent-generating process. The electrolytic process provides an acid leachant and an alkali hydroxide, with the alkali hydroxide then available for use either directly as a precipitant in the hydrometallurgical steps, or available for conversion by carbon capture to an alkali metal carbonate that can in turn be used as the precipitant in the selective hydrometallurgical steps. NEGATIVE EMISSION MATERIALS|NEGATIVE EMISSIONS MAT|NEGATIVE EMISSIONS MATERIALS (EP4251775)|Negative Emissions Materials, Inc.|(EP4251775)|Negative Emissions Materials, Inc. ([US])|(US20240002973)|NEGATIVE EMISSIONS MATERIALS, INC. ([US])|(WO2022/113025)|NEGATIVE EMISSIONS MATERIALS, INC. ([US])|(WO2022/113025)|NEGATIVE EMISSIONS MATERIALS, INC. ([US])||(JP2023553314)|Negative Emissions Materials, Inc.|(CN116802326)|NEGATIVE EMISSION MATERIALS CORPORATION ([US])|(ZA202305467)|NEGATIVE EMISSIONS MATERIALS, INC.|(AEP6001220/2023)|Negative Emissions Materials Inc ([US])|(IN202317042083)|NEGATIVE EMISSIONS MATERIALS INC|(AU2021389080)|NEGATIVE EMISSIONS MATERIALS, INC.|(AU2021389080)|NEGATIVE EMISSIONS MATERIALS, INC.|(HK40100255)|NEGATIVE EMISSIONS MATERIALS INC ([US])|(VN98973)|NEGATIVE EMISSIONS MATERIALS INC ([US])|(CR20230285)|NEGATIVE EMISSIONS MATERIALS, INC.|(CL2023001495)|NEGATIVE EMISSIONS MATERIALS, INC.|(ECSP23046201)|NEGATIVE EMISSIONS MATERIALS, INC.|(PE20231629)|NEGATIVE EMISSIONS MATERIALS, INC.|(TH2301002998)|Negative Emissions Materials, Inc. (entity incorporated under the laws of the United States)|(DOP2023000105)|NEGATIVE EMISSIONS MATERIALS, INC.|(KR10-2023-0110773)|Negative Emission Materials Inc. ([US])|(CO2023007635)|NEGATIVE EMISSIONS MATERIALS, INC.|(IL303119)|NEGATIVE EMISSIONS MATERIALS, INC. ([US])|(SG11202303717V)|NEGATIVE EMISSIONS MATERIALS INC|(BR112023010037)|NEGATIVE EMISSIONS MATERIALS INC ([US])||(ID2023/04650)|NEGATIVE EMISSIONS MATERIALS INC|(MX2023006141)|NEGATIVE EMISSIONS MATERIALS, INC.|(CA3198500)|NEGATIVE EMISSIONS MATERIALS, INC. ([US]) LEY JEREMY WILLIAM|DREISINGER DAVID (EP4251775)|LEY, Jeremy William|DREISINGER, David|(EP4251775)|LEY, Jeremy William|DREISINGER, David (EP4251775)|De Clercq & Partners ([BE])|Reg. Nb: 101331366|(JP2023553314)|ASAMURA IP P.C.|Reg. Nb: 110000855|(CN116802326)|LI NA;LIFANG & PARTNERS|Reg. Nb: 11330|(AEP6001220/2023)|Gowling WLG IP LCC|Reg. Nb: 759390|(AU2021389080)|James & Wells Intellectual Property ([AU])|(HK40100255)|ONC LAWYERS ([HK])|(VN98973)|Vision and Partnership Company Limited|(TH2301002998)|Mr. Sattayapol Satjadechan Mr. Krittawat Chainapasak|(KR10-2023-0110773)|KIM, JIN HOI|KIM, TAE HONG|(IL303119)|SHILON ZUCKERSTEIN & CO. ([IL])|(ID2023/04650)|Emirsyah Dinar|(CA3198500)|GOWLING WLG (CANADA) LLP ([CA]) (US20240002973)|The use of Mg(OH)2 to form MgCO3 by contact with air containing CO2 can in some circumstances suffer from unfavourable kinetics.| (US20240002973)|1 . A process for processing a comminuted mineral feedstock, comprising: a) leaching metal values from the comminuted mineral feedstock with an acid leachant, to produce a solid siliceous residue and a loaded leach solution; b) precipitating iron and/or aluminum from the loaded leach solution with addition of: a first alkali metal carbonate precipitant, to produce a carbon dioxide off gas, or, a first alkali hydroxide precipitant, to produce an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate product; c) precipitating nickel and/or cobalt from the Fe/Al depleted solution or from a Ni/Co ion exchange eluant obtained from the Fe/Al depleted solution by selective extraction of nickel and/or cobalt on an ion exchange medium, wherein the precipitating is with addition of: a second alkali metal carbonate or bicarbonate precipitant, or, a second alkali hydroxide precipitant, to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate or hydroxide precipitate product; d) before or after step (c), precipitating iron and/or aluminum and/or manganese from the Ni/Co depleted solution with addition of an oxidant and with addition of: a third alkali metal carbonate or bicarbonate precipitant, or, a third alkali hydroxide precipitant, to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product; e) precipitating magnesium from the Fe/Al/Mn depleted solution with addition of: a fourth alkali hydroxide precipitant, or a fourth alkali metal carbonate or bicarbonate precipitant, to produce a Mg-depleted solution and a magnesium hydroxide or carbonate precipitate product; f) subjecting the Mg-depleted solution to an electrolysis process to produce the acid leachant and: one or more of the alkali hydroxide precipitants, or an alkali hydroxide product.| (US20240002973)|Process of the invention accordingly provide for the use of less carbon intensive nickel, iron, calcium and magnesium hydroxides or carbonates, as well as olivine and basaltic sand material, including amorphous silicates, in marketable products.|The invention is in the field of inorganic chemistry, integrating electrochemical processes with steps of hydrometallurgical value extraction and carbon dioxide capture.| (US20240002973)|ALKALI HYDROXIDE PRECIPITANT(100,41)|COMMINUTED MINERAL FEEDSTOCK(100,14)|CARBON SEQUESTRATION(100,6)|METAL VALUE(100,4)|CARBON SEQUESTRATION INTEGRATION(100,1)|HYDROMETALLURGICAL RECOVERY(100,1)|METAL VALUE HYDROMETALLURGICAL RECOVERY(100,1)|HYDROXIDE PRECIPITANT(79,41)|BICARBONATE PRECIPITANT(79,33)|PRECIPITATING IRON(49,13)|UNFAVORABLE KINETICS(44,1)|ACID LEACHANT(43,19)|PRECIPITATING NA2CO3 HYDRATE(38,2)|ALKALI HYDROXIDE PRODUCT(34,16)|NICKEL SAPROLITE ORE(31,3)|PRECIPITANT(29,17)|HEMATITE PRODUCT PRECIPITATION(29,4)|PRECIPITATING NICKEL(29,3)|HYDROXIDE PRODUCT(28,16)|SOLID SILICEOUS RESIDUE(27,9)|MAGNESIUM PRECIPITATION(27,5)|ALKALI METAL CARBONATE(26,44)|ELECTROLYSIS(26,11)|AMORPHOUS SILICATE(25,3)|SOLID SILICEOUS RESIDUE ALKALIZATION(24,3)|CARBON INTENSIVE NICKEL(24,2)|HYDROMETALLURGICAL VALUE EXTRACTION(23,15)|MARKETABLE PRODUCT(23,1)|MG DEPLETED SOLUTION(22,18)|FE AL DEPLETED SOLUTION(21,13)|ASBESTOS ORE(21,3)|IRON ALKALIZATION(21,3)|OLIVINE ORE(21,3)|MAFIC MINERAL(21,2)|SOLID NA2CO3 CRYSTALIZER PRODUCT(20,6)|CO2(19,38)|PRECIPITATING CALCIUM(19,2)|BASALT IC SAND MATERIAL(19,1)|SCRUBBING SOLUTION(18,9)|COBALT HYDROXIDE PRECIPITATE(18,1)|TAILING(17,7)|ELECTROLYTIC GENERATION(17,2)|OLIVINE(16,5)|ALKALI METAL(15,47)|PRECIPITATION(15,7)|COBALT(14,10)|HEMATITE SEED MATERIAL(14,6)|MAGNESIUM HYDROXIDE(13,10)|INORGANIC CHEMISTRY(13,1)|CARBON DIOXIDE CAPTURE(12,11)|COMMINUTING(12,5)|CRYSTALIZATION(12,4)|ELUANT(12,3)|PURIFIED NICKEL PRODUCT(12,3)|CARBON DIOXIDE(11,31)|MANGANESE(11,6)|MANGANESE HYDROXIDE(11,5)|SCRUBBING CARBON DIOXIDE(11,5)|ION EXCHANGE MEDIUM(11,3)|WOLLASTONITE(11,3)|MAGNESIUM CARBONATE PRECIPITATE PRODUCT(11,2)|ULTRAMAFIC ROCK(11,2)|FE AL(10,21)|NI CO(10,18)|CALCIUM HYDROXIDE PRODUCT(10,12)|ALUMINUM HYDROXIDE(10,11)|ION EXCHANGE(10,10)|OXIDANT(10,6)|COBALT CARBONATE(10,5)|LEACHING METAL(10,3)|NI CO ION EXCHANGE(10,3)|ELECTROCHEMICAL(10,2)|MGCO3(9,7)|ELECTROLYTE SALT(9,6)|MIXED NI CO HYDROXIDE(9,2)|SODIUM HYPOCHLORITE NAOCL(9,2)|SALT SPLITTING(9,1)|NA2SO4(8,3)|CARBON CAPTURE PRODUCT(8,2)|H2SO(7,9)|ALUMINUM PRECIPITATION(7,6)|CHLORALKALI ELECTROCHEMICAL(7,6)|NAHCO3(7,4)|NICKEL VALUE(7,2)|SAPROLITE MATERIAL(7,2)|CRUSHED ORE FERROMAGNETIC CONTENT(7,1)|CARBON SOURCE(6,8)|CARBON DIOXIDE OFF GAS(6,7)|OFF GAS(6,7)|MG PRECIPITATION(6,3)|NI CO MHP PRECIPITATION(6,3)|AMORPHOUS SILICA RESIDUE(6,2)|ELECTROLYTIC REAGENT GENERATING(6,2)|CARBON INTENSIVE NICKEL COPRODUCTION(6,1)|MGCO3 MINERALIZATION(6,1)|NA2CO3 PRECIPITANT(6,1)|PARTLY LEACHED ORE(6,1)|STANDARD CHLORALKALI BRINE PRETREATMENT(6,1)|ULTRAMAFIC FEEDSTOCK(6,1)|CEMENT MANUFACTURE(5,3)|CHLOR ALKALI PLANT(5,2)|CO2 ADDITION(5,2)|IRON PRECIPITATION(5,2)|MINERAL ACID(5,2)|MIXED HYDROXIDE PRECIPITATE(5,2)|ADSORBENT REGENERATION(5,1)|ALKALI REAGENT RECYCLING(5,1)|CARBON INTENSIVE AMORPHOUS SILICATE(5,1)|MGCO3 PRECIPITATION(5,1)|STAGE MHP PRECIPITATION(5,1)|TRIVALENT CATION(5,1)|CRUSHING(4,3)|ELECTROLYTIC(4,2)|ELECTROLYTIC REACTANT REGENERATION(4,2)|MN HYDROXIDE(4,2)|BRINE SATURATION EVAPORATION(4,1)|CARBON HEAVY PYROMETALLURGY(4,1)|CO2 CONCENTRATED STREAM(4,1)|COARSE SEPARABLE PRECIPITATE(4,1)|CONCENTRATED CO2 STREAM(4,1)|GASEOUS CARBON DIOXIDE SEQUESTRATION(4,1)|HCL LEACHING PRODUCT(4,1)|MAFIC SAND INPUT(4,1)|MAGNETIC BENEFICIATION(4,1)|MAGNETITE MANUFACTURE(4,1)|MANGANESE SCRUBBING(4,1)|MAXIMIZE EXTRACTION(4,1)|MAXIMIZE OXIDATIVE REMOVAL(4,1)|MAXIMIZE PRECIPITATION(4,1)|MGCO3 RECOVERY(4,1)|MINERAL CARBONATE(4,1)|MINERAL SEED(4,1)|NICKEL COBALT PRECIPITATION(4,1)|PLURAL REFERENT(4,1)|POLISH FILTRATION(4,1)|PRECIPITATION TANK(4,1)|PURITY MG DEPLETED BRINE(4,1)|RECYCLED BRINE SOLUTION(4,1)|REFRACTORY MARKET(4,1)|SEA ENVIRONMENT(4,1)|SEED RECYCLING(4,1)|SILICA RICH RESIDUE(4,1)|SILICEOUS RESIDUE(4,1)|SPECIES PURIFICATION(4,1)|SYNTHETIC BRUCITE PRODUCTION(4,1)|TREATING NA2SO(4,1)|UNTREATED MAFIC ROCK(4,1)|HYDROMETALLURGICAL(3,11)|KOH(3,4)|2H2O ALKALI METAL CARBONATE(3,2)|ALKALIZATION(3,2)|BASALTIC SAND MATERIAL(3,2)|CA DEPLETED SOLUTION(3,2)|CARBON DIOXIDE GAS SCRUBBING(3,2)|CO2 SCRUBBING(3,2)|CRYSTALIZER(3,2)|HCL SOLUTION(3,2)|IMPURITY(3,2)|IRON REMOVAL(3,2)|LEACHING TEMPERATURE(3,2)|MAGNESIUM HYDROXIDE PRECIPITATE PRODUCT(3,2)|NAOH SOLUTION(3,2)|NI CO PRECIPITATION(3,2)|ACID LEACHING CHEMISTRY(3,1)|ALKALINE SPECIES(3,1)|BARREN SOLUTION(3,1)|CO2 ENRICHED SOLUTION(3,1)|COCL2 SALT(3,1)|CONTAMINANT(3,1)|ELECTROLYSIS CHLORINE GAS PRODUCT(3,1)|ENHANCE PRECIPITATION(3,1)|FE AL NEUTRALIZATION(3,1)|FE AL PRECIPITATION RESIDUE(3,1)|HYDROMETALLURGICAL VALUE RECOVERY(3,1)|ION EXCHANGE ELUANT(3,1)|ION EXCHANGE SOFTENING(3,1)|IRON PRECIPITATE PRODUCTION(3,1)|IRON RESIDUE(3,1)|MAGNETIC SEPARATOR(3,1)|MANGANESE REMOVAL(3,1)|MAXIMIZE REMOVAL(3,1)|METAL CARBONATE PRECIPITANT(3,1)|MG CARBONATE(3,1)|MG HYDROXIDE(3,1)|MGCO3 FORMATION(3,1)|MGSIO RATIO(3,1)|MINERAL DISSOLUTION PRODUCT(3,1)|NACL TREATMENT(3,1)|NAOH MANUFACTURE(3,1)|PERFORMANCE CONCRETE(3,1)|PH MODULATOR(3,1)|SEQUESTERING CARBON DIOXIDE(3,1)|STAGE PRECIPITATE(3,1)|STREAM CONCENTRATION(3,1)|SULFATE SALT(3,1)|SULFURIC ACID LEACHANT(3,1)|TERMINAL ACIDITY(3,1)|TIRE MANUFACTURING INDUSTRY(3,1)|WEAKLY ACIDIC SOLUTION(3,1)|PROCESS INTEGRATION(2,11)|GRINDING(2,3)|MGSO(2,3)|ADDRESSING ANTHROPOGENIC CLIMATE CHANGE(2,1)|ALKALI METAL PRECIPITANT(2,1)|ALUMINUM CONTENT(2,1)|APPROXIMATION(2,1)|CALCINATION(2,1)|CARBON INTENSIVE CONSTRUCTION(2,1)|CEMENT CARBON INTENSITY(2,1)||(WO2022/113025)|CARBON SEQUESTRATION(100,1)|CARBON SEQUESTRATION INTEGRATION(100,1)|HYDROMETALLURGICAL RECOVERY(100,1)|METAL VALUE(100,1)|METAL VALUE HYDROMETALLURGICAL RECOVERY(100,1)|HYDROMETALLURGICAL(63,2)|ALKALI HYDROXIDE(62,2)|PRECIPITANT(50,2)|HYDROMETALLURGICAL VALUE EXTRACTION(44,1)|ACID LEACHANT(43,1)|CARBON CAPTURE(24,2)|CARBON CAPTURE PRODUCT(21,1)||(WO2022/113025)|CARBON SEQUESTRATION(100,1)|CARBON SEQUESTRATION INTEGRATION(100,1)|HYDROMETALLURGICAL RECOVERY(100,1)|METAL VALUE(100,1)|METAL VALUE HYDROMETALLURGICAL RECOVERY(100,1)|HYDROMETALLURGICAL(63,2)|ALKALI HYDROXIDE(62,2)|PRECIPITANT(50,2)|HYDROMETALLURGICAL VALUE EXTRACTION(44,1)|ACID LEACHANT(43,1)|CARBON CAPTURE(24,2)|CARBON CAPTURE PRODUCT(21,1)||(CN116802326)|BICARBONATE PRECIPITANT(100,37)|CARBON SEQUESTRATION(100,6)|MINERAL RAW MATERIAL(100,6)|CARBON SEQUESTRATION INTEGRATION(100,1)|HYDROMETALLURGICAL RECOVERY(100,1)|METAL VALUE(100,1)|METAL VALUE HYDROMETALLURGICAL RECOVERY(100,1)|CRUSHED MINERAL FEEDSTOCK(86,7)|PRECIPITANT(60,58)|PRECIPITATING IRON(57,13)|COMMINUTED MINERAL FEEDSTOCK(54,5)|FERRIC HYDROXIDE(50,10)|PRECIPITATION PRODUCT(44,22)|PRECIPITATING NICKEL(42,4)|SOLID SILICEOUS RESIDUE(41,11)|ALKALI METAL HYDROXIDE(40,80)|RECYCLING BRINE(38,3)|MAGNESIUM PRECIPITATION(36,6)|CARBON CONCRETE BUILDING(32,1)|NI EXTRACTION(32,1)|ALKALI METAL CARBONATE(31,47)|PRECIPITATING ALUMINUM(31,1)|ALKALI METAL(29,128)|ALUMINUM HYDROXIDE(28,21)|ALUMINUM OXIDE PRECIPITATION PRODUCT(28,6)|COBALT HYDROXIDE PRECIPITATION PRODUCT(28,3)|CONCRETE BUILDING(28,1)|COPRODUCE NICKEL HYDROXIDE(28,1)|MG DEPLETED SOLUTION(27,19)|HEMATITE PRODUCT(27,5)|MANGANESE HYDROXIDE PRECIPITATION PRODUCT(26,5)|ACID LEACHING(25,19)|FE AL LEAN SOLUTION(25,12)|HYDROMETALLURGICAL VALUABLE EXTRACTION(24,14)|OXIDANT(24,6)|SLIDING MAGNESIUM HYDROXIDE(22,5)|PURIFIED NICKEL PRODUCT(22,4)|PRECIPITATING SODIUM(22,1)|ELECTROLYSIS(21,8)|NICKEL CARBONATE(21,8)|AMORPHOUS SILICATE(21,4)|MAGNESIUM CARBONATE PRECIPITATE PRODUCT(21,1)|MARKETABLE PRODUCT(21,1)|PRECIPITATE PRODUCTION(21,1)|SLIDING ELECTRICAL BATTERY(21,1)|SUPPORT TRANSITIONING(21,1)|MAGNESIUM CARBONATE(20,8)|COBALT CARBONATE(20,7)|COBALT(20,6)|OLIVINE ORE(20,2)|DYNAMICS(20,1)|SLIDING REAGENT GENERATION(20,1)|PRECIPITATION(19,11)|FERRIC OXIDE(19,9)|HEMATITE SEED MATERIAL(19,7)|ASBESTOS ORE(19,2)|HEMATITE PRODUCT PRECIPITATION(19,2)|HYDROMETALLURGICAL VALUE EXTRACTION(19,1)|ELUATE(18,4)|HEMATITE PRODUCT PRECIPITATE(18,2)|OLIVINE SLIDING WURTZITE MATERIAL(18,1)|ALUMINUM OXIDE(17,10)|COBALT HYDROXIDE(17,6)|PRECIPITATING CALCIUM(17,2)|BRINE SOLUTION(17,1)|SLIDING IRON(17,1)|NI CO(16,16)|HEMATITE(16,10)|MANGANESE(16,7)|TAILING(16,7)|MANGANESE HYDROXIDE(16,6)|SCRUBBING SOLUTION(16,5)|ION EXCHANGE MEDIUM(16,4)|COBALT HYDROXIDE PRECIPITATE(16,1)|COCONTAINING PRODUCT(16,1)|NAOH SOLUTION(16,1)|ION EXCHANGE(15,12)|NICKEL HYDROXIDE(15,8)|COMMINUTION(15,4)|LEACHING METAL(15,4)|ROUTE(15,3)|ELECTRIC VEHICLE SLIDING BATTERY(15,1)|ELECTROLYTIC PRODUCTION(15,1)|MAGNESIUM IRON ORE(15,1)|FE AL(14,21)|NI CO ION EXCHANGE(14,4)|NICKEL VALUE(14,3)|MAGNESIUM IRON ROCK(14,1)|SLIDING WURTZITE MATERIAL(13,1)|MAGNESIUM HYDROXIDE(12,11)|MAGNESIUM CARBONATE PRECIPITATION PRODUCT(12,1)|CARBON DIOXIDE(11,30)|SOLID SODIUM(11,7)|COMMINUTING(11,2)|WOLLASTONITE(10,3)|CARBON DIOXIDE WASTE GAS(10,1)|DECARBONIZE FIELD(10,1)|CALCIUM HYDROXIDE PRODUCT(9,11)|CRYSTALIZATION(9,6)|NICKEL SAPROLITE ORE(9,2)|WASTE GAS(9,1)|MGCO(8,10)|MIXED NI CO HYDROXIDE(8,2)|SODIUM HYPOCHLORITE NAOCL(8,2)|SUPPORT TREATMENT(8,1)|HYDRATE(7,6)|ELECTROLYTE SALT(7,5)|IRON PRECIPITATION(7,4)|SALT SPLITTING(7,2)|ELECTRIC VEHICLE(7,1)|SUPER FERRIMAGNESIUM ROCK(7,1)|CARBON SOURCE(6,8)|CHLOR ALKALI(6,7)|NI CO MHP PRECIPITATION(6,3)|AMORPHOUS SILICA RESIDUE(6,2)|BASTARD SAND(6,2)|IRON SLIDING ALUMINUM PRECIPITATION(6,2)|SAPROLITE MATERIAL(6,2)|CRUSHED ORE FERROMAGNETIC CONTENT(6,1)|CEMENT MANUFACTURE(5,3)|COCONTAINING SOLUTION(5,3)|MG PRECIPITATION(5,3)|MIXED HYDROXIDE PRECIPITATE(5,2)|PH CONTROL(5,2)|ACCELERATE WEATHERING REACTION(5,1)|ALKALI HYDROXIDE PRECIPITANT(5,1)|BRINE SATURATION EVAPORATION SLIDING SOFTENING(5,1)|CARBON CAPTURE ELECTROLYTIC(5,1)|ENHANCE MARINE ALKALINITY(5,1)|FERRIMAGNESIUM ORE(5,1)|LEACHED ORE(5,1)|MINERAL ACID(5,1)|MN HYDROXIDE PRECIPITATION(5,1)|MULTISTAGE LEACHING(5,1)|NICKEL SLIDING COBALT PRECIPITATION(5,1)|STANDARD CHLORALKALI BRINE PRETREATMENT(5,1)|STRONG BASE(5,1)|STRUCTURING AGGREGATE(5,1)|TRIVALENT CATION(5,1)|BICARBONATE(4,4)|WASHING SOLUTION(4,4)|ELECTROLYTIC REACTANT REGENERATION(4,2)|MAGNESIUM RECOVERY(4,2)|MGCO FORMATION(4,2)|CARBANION HYDROXIDE(4,1)|CARBON AMORPHOUS SILICATE(4,1)|HYDROGEN SALT PRECIPITANT(4,1)|MAXIMIZE OXIDATIVE REMOVAL(4,1)|MN HYDROXIDE PRECIPITATE(4,1)|MOISTURE ENTRAINMENT(4,1)|PLURAL REFERENT(4,1)|PRECIPITANT NAOH(4,1)|PRECIPITATE PRECIPITATION(4,1)|PURIFIED NICKEL SLIDING COBALT(4,1)|PURITY MG DEPLETED BRINE(4,1)|SILICA RICH RESIDUE(4,1)|STAGE MHP PRECIPITATION(4,1)|UNTREATED IRON MAGNESIUM ROCK(4,1)|ALUMINUM(3,18)|IRON REMOVAL(3,3)|CA DEPLETED SOLUTION(3,2)|CARBON DIOXIDE CAPTURE(3,2)|IMPURITY(3,2)|LEACHING TEMPERATURE(3,2)|MN SOLUTION(3,2)|NEUTRALIZING(3,2)|NI CO PRECIPITATION(3,2)|PH ADJUSTMENT(3,2)|PRODUCT CRYSTAL(3,2)|SCRUBBING CARBON DIOXIDE(3,2)|SLIDING NAOH(3,2)|SULFURIC ACID LEACHING(3,2)|ALKALINE HYDROXIDE(3,1)|CALCINATION SLIDING(3,1)|CHLOR ALKALI FACILITY(3,1)|CHLOR ALKALI PLANT(3,1)|COARSE SEPARABLE PRECIPITATE(3,1)|CRACKING PLANT(3,1)|DOCUMENT SLIDING PUBLICATION(3,1)|ELECTROLYTIC GENERATION(3,1)|ENHANCE PRECIPITATION(3,1)|FERRIC HYDROXIDE PRECIPITATED PRODUCT(3,1)|FIRE MARKET(3,1)|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)|HCL LEACHING PRODUCT(3,1)|MAGNETIC ENRICHMENT(3,1)|MAGNETITE MANUFACTURE(3,1)|MANGANESE WASHING(3,1)|MAXIMIZE PRECIPITATION(3,1)|MINERAL CARBONATE(3,1)|MINERAL SEED(3,1)|NAOH SLIDING CL(3,1)|OCEAN ALKALINITY SUPPORT(3,1)|PRECIPITANT SLIDING ACID LEACHING(3,1)|PRECIPITATING IRON SLIDING ALUMINUM(3,1)|PRECIPITATION TANK(3,1)|PRODUCING SILICEOUS RESIDUE(3,1)|PRODUCING SYNTHETIC BRUCITE(3,1)|RECYCLED BRINE SOLUTION(3,1)|SEED RECYCLING(3,1)|SLIDING NICKEL COBALT PRECIPITATION(3,1)|INORGANIC RAW MATERIAL(2,15)|PROCESS INTEGRATION(2,11)|HYDROMETALLURGICAL(2,10)|KOH(2,4)|LOW CARBON(2,4)|MGCL(2,4)|ELECTROLYSIS(2,3)|NACL(2,3)|NICL(2,3)|OXIDIZING AGENT(2,3)|ADDRESSING(2,1)|ADSORBENT(2,1)|ALKALI ADJUSTMENT(2,1)|ALKALI CARBONATE(2,1)|ALKALI METAL PRECIPITANT(2,1)|ALKALINE SUBSTANCE(2,1)|ALKALIZATION(2,1)|ALUMINUM HYDROXIDE PRECIPITATED PRODUCT(2,1)|CALCIUM HYDROXIDE ADDRESS(2,1)|CARBON DIOXIDE GAS SCRUBBING(2,1)|CARBON DIOXIDE SCRUBBING(2,1)|CARBON HEAVY PYROMETALLURGY SUPPORT(2,1)|CEMENT CARBON STRENGTH(2,1)|CEMENTATION(2,1)|CO SUBSTANCE(2,1)|COBALT CARBONATE PRECIPITATED PRODUCT(2,1)|COCONTAINING SUPPORT(2,1)|CONTAMINANT(2,1)|COUNTERCURRENT MOVEMENT(2,1)|ELECTROLYTICALLY DERIVED BARREN SOLUTION(2,1)|FE AL NEUTRALIZATION(2,1)|FE AL PRECIPITATION RESIDUE(2,1)|HYDROMETALLURGICAL VALUE RECOVERY(2,1)|HYDROMETALLURGY(2,1)|ION EXCHANGE ELUATE(2,1)|ION EXCHANGE SOFTENING(2,1)|IRON MAGNESIUM FEEDSTOCK(2,1)|IRON PRECIPITATE PRODUCTION(2,1)|IRON RESIDUE(2,1)|LEACHING CONDITION(2,1)|LESSER CARBON CALCIUM HYDROXIDE(2,1)|LOADED LEACHING SOLUTION(2,1)|LOW CARBON ECONOMY(2,1)|MAGNETIC SEPARATOR(2,1)|MANGANESE REMOVAL(2,1)|METAL CARBONATE PRECIPITANT(2,1)|MG CARBONATE(2,1)|MG HYDROXIDE(2,1)|MG NI EXTRACTION(2,1)|MINERAL DISSOLUTION PRODUCT(2,1)|NICKEL CHLORIDE SLIDING COBALT(2,1)|ORE SLIDING(2,1)|PERFORMANCE CONCRETE(2,1)|PRECIPITATE IRON(2,1)|SALT CRACKING(2,1)|SEPARATION SLIDING WASHING(2,1)|SEQUESTERING CARBON(2,1)|SLIDING VARIANT(2,1)|STAGE PRECIPITATE(2,1)|SUPER IRON MAGNESIUM(2,1)|TOAPPLICATION(2,1)|TREATING SODIUM(2,1)|WASHING IRON(2,1)|WEAK ACIDIC SOLUTION(2,1)||(IN202317042083)|ALKALI HYDROXIDE PRECIPITANT(100,46)|CARBON SEQUESTRATION(100,6)|METAL VALUE(100,4)|PROCESSING COMMINUTED MINERAL FEEDSTOCK(100,4)|CARBON SEQUESTRATION INTEGRATION(100,1)|HYDROMETALLURGICAL RECOVERY(100,1)|METAL VALUE HYDROMETALLURGICAL RECOVERY(100,1)|HYDROXIDE PRECIPITANT(80,46)|BICARBONATE PRECIPITANT(80,37)|COMMINUTED MINERAL FEEDSTOCK(76,14)|PRECIPITATING IRON(51,16)|ACID LEACHANT(41,21)|UNFAVORABLE KINETICS(37,1)|ALKALI HYDROXIDE PRODUCT(33,18)|PRECIPITATING NA2CO3 HYDRATE(32,2)|SOLID SILICEOUS RESIDUE(31,11)|PRECIPITATING NICKEL(31,4)|SOLID SILICEOUS RESIDUE ALKALIZATION(30,4)|MAGNESIUM PRECIPITATION(29,6)|HYDROXIDE PRODUCT(27,18)|IRON ALKALIZATION(27,4)|NICKEL SAPROLITE ORE(26,3)|ALKALI METAL CARBONATE(25,50)|ELECTROLYSIS(25,12)|HEMATITE PRODUCT PRECIPITATION(25,4)|PRECIPITANT(24,17)|FE AL DEPLETED SOLUTION(23,16)|MG DEPLETED SOLUTION(22,19)|AMORPHOUS SILICATE(21,3)|CARBON INTENSIVE NICKEL(21,2)|HYDROMETALLURGICAL VALUE EXTRACTION(19,15)|MARKETABLE PRODUCT(19,1)|CO2(18,37)|ASBESTOS ORE(18,3)|OLIVINE ORE(18,3)|MAFIC MINERAL(18,2)|SOLID NA2CO3 CRYSTALIZER PRODUCT(17,6)|COBALT(16,12)|PRECIPITATION(16,8)|PURIFIED NICKEL PRODUCT(16,4)|PRECIPITATING CALCIUM(16,2)|BASALT IC SAND MATERIAL(16,1)|SCRUBBING SOLUTION(15,9)|HEMATITE SEED MATERIAL(15,7)|COBALT HYDROXIDE PRECIPITATE(15,1)|ALKALI METAL(14,53)|TAILING(14,7)|COMMINUTING(14,6)|OLIVINE(14,5)|ELUANT(14,4)|MAGNESIUM CARBONATE PRECIPITATE PRODUCT(14,3)|ELECTROLYTIC GENERATION(14,2)|COBALT CARBONATE(13,7)|ALUMINUM HYDROXIDE(12,16)|MAGNESIUM HYDROXIDE(12,12)|MANGANESE(12,7)|MANGANESE HYDROXIDE(12,6)|ION EXCHANGE MEDIUM(12,4)|CARBON DIOXIDE(11,33)|FE AL(11,24)|NI CO(11,21)|ION EXCHANGE(11,12)|LEACHING METAL(11,4)|SEQUESTERING CARBON DIOXIDE(11,2)|INORGANIC CHEMISTRY(11,1)|CARBON DIOXIDE CAPTURE(10,11)|CRYSTALIZATION(10,4)|NI CO ION EXCHANGE(10,4)|NICKEL VALUE(10,3)|ULTRAMAFIC ROCK(10,2)|SCRUBBING CARBON DIOXIDE(9,5)|WOLLASTONITE(9,3)|ELECTROCHEMICAL(9,2)|CALCIUM HYDROXIDE PRODUCT(8,12)|MGCO3(8,10)|ELECTROLYTE SALT(8,6)|OXIDANT(8,6)|SALT SPLITTING(8,1)|CARBON CAPTURE PRODUCT(7,2)|MIXED NI CO HYDROXIDE(7,2)|H2SO(6,9)|CARBON DIOXIDE OFF GAS(6,8)|OFF GAS(6,8)|ALUMINUM PRECIPITATION(6,6)|CHLORALKALI ELECTROCHEMICAL(6,6)|IRON PRECIPITATION(6,4)|NAHCO3(6,4)|SAPROLITE MATERIAL(6,2)|CRUSHED ORE FERROMAGNETIC CONTENT(6,1)|CARBON SOURCE(5,8)|MG PRECIPITATION(5,3)|NI CO MHP PRECIPITATION(5,3)|AMORPHOUS SILICA RESIDUE(5,2)|ELECTROLYTIC REAGENT GENERATING(5,2)|CARBON INTENSIVE NICKEL COPRODUCTION(5,1)|MGCO3 MINERALIZATION(5,1)|NA2CO3 PRECIPITANT(5,1)|PARTLY LEACHED ORE(5,1)|STANDARD CHLORALKALI BRINE PRETREATMENT(5,1)|ULTRAMAFIC FEEDSTOCK(5,1)|NA2SO4(4,9)|CEMENT MANUFACTURE(4,3)|CO2 ADDITION(4,2)|MINERAL ACID(4,2)|MIXED HYDROXIDE PRECIPITATE(4,2)|ADSORBENT REGENERATION(4,1)|ALKALI REAGENT RECYCLING(4,1)|CARBON HEAVY PYROMETALLURGY(4,1)|CARBON INTENSIVE AMORPHOUS SILICATE(4,1)|CHLORALKALI PLANT(4,1)|MANGANESE SCRUBBING(4,1)|MAXIMIZE OXIDATIVE REMOVAL(4,1)|MGCO3 PRECIPITATION(4,1)|MGCO3 RECOVERY(4,1)|PLURAL REFERENT(4,1)|POLISH FILTRATION(4,1)|PURITY MG DEPLETED BRINE(4,1)|REFRACTORY MARKET(4,1)|SILICEOUS RESIDUE(4,1)|STAGE MHP PRECIPITATION(4,1)|TRIVALENT CATION(4,1)|UNTREATED MAFIC ROCK(4,1)|CRUSHING(3,3)|ELECTROLYTIC(3,2)|ELECTROLYTIC REACTANT REGENERATION(3,2)|MAGNESIUM RECOVERY(3,2)|MANGANESE REMOVAL(3,2)|MN HYDROXIDE(3,2)|BRINE SATURATION EVAPORATION(3,1)|CHLOR ALKALI PLANT(3,1)|CO2 CONCENTRATED STREAM(3,1)|COARSE SEPARABLE PRECIPITATE(3,1)|CONCENTRATED CO2 STREAM(3,1)|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)|HCL LEACHING PRODUCT(3,1)|MAFIC SAND INPUT(3,1)|MAGNETIC BENEFICIATION(3,1)|MAGNETITE MANUFACTURE(3,1)|MAXIMIZE EXTRACTION(3,1)|MAXIMIZE PRECIPITATION(3,1)|MINERAL CARBONATE(3,1)|MINERAL SEED(3,1)|NICKEL COBALT PRECIPITATION(3,1)|PRECIPITATION TANK(3,1)|RECYCLED BRINE SOLUTION(3,1)|SEA ENVIRONMENT(3,1)|SEED RECYCLING(3,1)|SILICA RICH RESIDUE(3,1)|SPECIES PURIFICATION(3,1)|SYNTHETIC BRUCITE PRODUCTION(3,1)|TREATING NA2SO(3,1)|HYDROMETALLURGICAL(2,11)|PROCESS INTEGRATION(2,11)|KOH(2,4)|GRINDING(2,3)|MGSO4(2,3)|3NA2SO(2,2)|ALKALIZATION(2,2)|BASALTIC SAND MATERIAL(2,2)|CA DEPLETED SOLUTION(2,2)|CARBON DIOXIDE GAS SCRUBBING(2,2)|CO2 SCRUBBING(2,2)|CRYSTALIZER(2,2)|HCL SOLUTION(2,2)|IMPURITY(2,2)|IRON REMOVAL(2,2)|LEACHING TEMPERATURE(2,2)|MAGNESIUM HYDROXIDE PRECIPITATE PRODUCT(2,2)|NAOH SOLUTION(2,2)|NEUTRALIZING(2,2)|NI CO PRECIPITATION(2,2)|ACID LEACHING CHEMISTRY(2,1)|ADDRESSING ANTHROPOGENIC CLIMATE CHANGE(2,1)|ALKALI METAL PRECIPITANT(2,1)|ALKALINE SPECIES(2,1)|ALUMINUM CONTENT(2,1)|APPROXIMATION(2,1)|BARREN SOLUTION(2,1)|CALCINATION(2,1)|CARBON INTENSIVE CONSTRUCTION(2,1)|CO2 ENRICHED SOLUTION(2,1)|CONTAMINANT(2,1)|ELECTROLYSIS CHLORINE GAS PRODUCT(2,1)|ENHANCE PRECIPITATION(2,1)|FE AL NEUTRALIZATION(2,1)|FE AL PRECIPITATION RESIDUE(2,1)|HYDROMETALLURGICAL VALUE RECOVERY(2,1)|ION EXCHANGE ELUANT(2,1)|ION EXCHANGE SOFTENING(2,1)|IRON PRECIPITATE PRODUCTION(2,1)|IRON RESIDUE(2,1)|MAGNESIUM HYDROXIDE PRECIPITATION(2,1)|MAGNETIC SEPARATOR(2,1)|MAXIMIZE REMOVAL(2,1)|METAL CARBONATE PRECIPITANT(2,1)|MG CARBONATE(2,1)|MG HYDROXIDE(2,1)|MGCO3 FORMATION(2,1)|MGDEPLETED SOLUTION(2,1)|MGSICU RATIO(2,1)|MINERAL DISSOLUTION PRODUCT(2,1)|NACL TREATMENT(2,1)|NAOH MANUFACTURE(2,1)|PERFORMANCE CONCRETE(2,1)|PH MODULATOR(2,1)|PURIFIED NICKEL(2,1)|STAGE PRECIPITATE(2,1)|STREAM CONCENTRATION(2,1)|SULFATE SALT(2,1)|SULFURIC ACID LEACHANT(2,1)|TERMINAL ACIDITY(2,1)|TIRE MANUFACTURING INDUSTRY(2,1)|WEAKLY ACIDIC SOLUTION(2,1)||(KR10-2023-0110773)|ALKALI HYDROXIDE PRECIPITANT(100,35)|GROUND MINERAL FEEDSTOCK(100,18)|CARBON SEQUESTRATION(100,5)|METAL FECES(100,4)|WET SMELTING(100,4)|METAL FECES RECOVERY(100,2)|CARBON SEQUESTRATION INTEGRATION(100,1)|BICARBONATE PRECIPITANT(83,27)|HYDROXIDE PRECIPITANT(80,35)|LOADED LEACHING SOLUTION(53,17)|SOLID SILICEOUS RESIDUE(45,12)|PRECIPITATING IRON(45,9)|PRECIPITATION PRODUCT(40,20)|PRECIPITATING NICKEL(39,4)|ALKALI HYDROXIDE PRODUCT(38,18)|ALKALI HYDROXIDE PRECIPITATE(36,7)|HYDROXIDE PRODUCT(31,18)|OXIDE PRECIPITATION PRODUCT(31,9)|ALKALI METAL CARBONATE(29,48)|MN DEPLETION SOLUTION(29,5)|FE AL DEPLETION SOLUTION(28,6)|MAGNESIUM PRECIPITATION(28,2)|HYDROXIDE PRECIPITATE(27,13)|HEMATITE ADDITION(27,1)|ELECTROLYSIS(26,14)|HEMATITE PRODUCT(26,5)|MANGANESE HYDROXIDE PRECIPITATION PRODUCT(26,4)|MG DEPLETED SOLUTION(24,16)|NI CO DEPLETION SOLUTION(24,10)|ACID LEACHING(23,23)|COMPENSATING CARBON HEAVY(23,1)|SEQUESTERING CARBON DIOXIDE(23,1)|PRECIPITANT(22,14)|BICARBONATE PRECIPITATE(22,7)|MAGNESIUM CARBONATE PRECIPITATION PRODUCT(22,2)|AMORPHOUS SILICATE(21,3)|ULTRAFERROUS ROCK(21,2)|ALKALI HYDROXIDE(20,18)|PURIFIED NICKEL PRODUCT(20,4)|HEMATITE PRODUCT PRECIPITATE(20,1)|COBALT(19,12)|SMELTING(19,5)|COBALT CARBONATE(18,7)|SMELTING FED BATCH EXTRACTION(18,3)|HEMATITE SEED MATERIAL(17,7)|OLIVINE(17,6)|ELUENT(17,4)|ASBESTOS ORE(17,3)|HYDROXIDE PRECIPITATION PRODUCT(17,3)|COBALT CARBONATE PRECIPITATION PRODUCT(17,2)|CARBON INTENSIVE CONSTRUCTION(17,1)|ALKALI METAL(16,51)|ALUMINUM HYDROXIDE(16,16)|FE AL DEPLETED SOLUTION(16,6)|CRYSTALIZER PRODUCT(16,5)|CARBONATE PRECIPITATION PRODUCT(16,4)|ELECTROCHEMICAL(16,2)|FERROUS MINERAL(16,2)|PRECIPITATING CALCIUM(16,2)|BRINE SOLUTION(16,1)|CO2(15,21)|LEACHING(15,8)|MANGANESE(15,7)|ION EXCHANGE MEDIUM(15,4)|CARBON INTENSIVE(15,3)|MAGNESIUM CARBONATE(15,2)|COBALT HYDROXIDE PRECIPITATE(15,1)|MARKET PRODUCT(15,1)|ION EXCHANGE(14,12)|MAGNESIUM HYDROXIDE(14,12)|MANGANESE HYDROXIDE(14,6)|FE AL(13,22)|GRINDING(13,8)|SOLID NA2CO3(13,7)|BRINE(13,6)|NI CO ION EXCHANGE(13,4)|WET SMELTING FECES EXTRACTION(13,4)|CO2 SCRUBBING CARBON DIOXIDE(13,2)|FED BATCH EXTRACTION(12,2)|METAL FEEDING(12,1)|CARBON DIOXIDE(11,31)|CARBON DIOXIDE CAPTURE(11,7)|PRECIPITATION(11,6)|BICARBONATE(11,5)|PRECIPITATE(11,5)|ALUMINUM HYDROXIDE PRECIPITATION PRODUCT(11,3)|2SO4BASED(11,1)|INORGANIC CHEMISTRY(11,1)|K2CO3BASED(11,1)|SCRUBBING SOLUTION(10,5)|BASALT(10,4)|CARBON NEGATIVE MAGNETIC(10,1)|OXIDIZING AGENT(9,9)|WOLLASTONITE(9,3)|2SO4BY(9,2)|FED BATCH(9,1)|WET SMELTING(8,11)|CALCIUM HYDROXIDE PRODUCT(8,10)|MG DEPLETING SOLUTION(8,4)|CARBON DIOXIDE OFF GAS(8,2)|PROCESS CONVENIENCE(8,1)|NI CO(7,9)|ELECTROLYSIS SALT(7,5)|OFF GAS(7,3)|CARBON CAPTURE PRODUCT(7,2)|ELECTROLYSIS(7,2)|METAL FED BATCH(7,2)|MIXED NI CO HYDROXIDE(7,2)|NAHCO3(7,2)|PH CONTROL(7,2)|SODIUM HYPOCHLORITE NAOCL(7,2)|MARINE ALKALINITY RISK(7,1)|ALUMINUM PRECIPITATION(6,6)|CHLORALKALI ELECTROCHEMICAL(6,6)|HYDRATE(6,6)|NA2CO3 CRYSTALIZATION(6,2)|OLIVINE ORE(6,2)|SAPROLITE MATERIAL(6,2)|ATMOSPHERE 2NA FROM2CO3TO(6,1)|NICKEL SAPROLITE ORE(6,1)|CARBON SOURCE(5,8)|NI CO MHP PRECIPITATION(5,3)|AMORPHOUS SILICA RESIDUE(5,2)|CARBON NEGATIVE(5,2)|ELECTROLYSIS REAGENT PRODUCING(5,2)|MN HYDROXIDE PRECIPITATE(5,2)|ENHANCED PH CONTROL(5,1)|LEACHED ORE(5,1)|MAXIMIZE OXIDATIVE ELIMINATION(5,1)|MG PRECIPITATION STAGE2CO3ADDING(5,1)|MGCO3 MINERALIZATION(5,1)|NA2CO3 PRECIPITANT(5,1)|STANDARD CHLORALKALI BRINE PRETREATMENT(5,1)|ULTRAFERROUS FEEDSTOCK(5,1)|ALUMINUM(4,29)|MAGNETITE(4,4)|MINERAL ACID(4,2)|MIXED HYDROXIDE PRECIPITATE(4,2)|RECYCLING HCL(4,2)|SEED RECYCLING(4,2)|ABRASIVE FILTRATION(4,1)|ACIDIC LEACHATE(4,1)|BASALT SAND(4,1)|CARBON INTENSIVE AMORPHOUS SILICATE(4,1)|CEMENT SUBSTITUTE(4,1)|CO2IS REPRESENTATION(4,1)|COBALT FECES(4,1)|H2AND CL2(4,1)|HCLPER DRY TON(4,1)|MANGANESE SCRUBBING(4,1)|MAXIMIZE GRANULARITY(4,1)|MGCO3ALTERNATIVE ROUTE(4,1)|MGCO3IS PLOT(4,1)|MINERAL FEEDSTOCK GROUND(4,1)|MULTISTAGE LEACHING(4,1)|NA2CO3IS MGCL2(4,1)|NA2CO3IS PLOT(4,1)|NAOH REGENERATION(4,1)|NAOHWITH MGCL2 SOLUTION(4,1)|NICKEL BASALT(4,1)|PLURAL REFERENT(4,1)|PURITY MG DEPLETED BRINE(4,1)|RECOVERY OF2CO3IS(4,1)|RICH SOLUTION2CO(4,1)|SILICEOUS RESIDUE(4,1)|STAGE MHP PRECIPITATION(4,1)|STRONG BASE(4,1)|TRIVALENT CATION(4,1)|NA2SO4(3,7)|WET SMELTING PROCESS REACTANT(3,6)|ALKALI PLANT(3,2)|CONCENTRATION CO2(3,2)|ELECTROLYSIS REACTANT REGENERATION(3,2)|IMPURITY(3,2)|MAGNESIUM RECOVERY(3,2)|MANGANESE REMOVAL(3,2)|SULFURIC ACID LEACHING(3,2)|BRINE SATURATION EVAPORATION(3,1)|COARSE SEPARABLE PRECIPITATE(3,1)|FERROMAGNETIC CONTENT(3,1)|HCL LEACHING PRODUCT(3,1)|IRON SAND DOSING(3,1)|MAXIMIZE EXTRACTION(3,1)|MAXIMIZE PRECIPITATION(3,1)|MINERAL CARBONATE(3,1)|MINERAL SEED(3,1)|NICKEL COBALT PRECIPITATION(3,1)|PRECIPITATION RESIDUE(3,1)|PRECIPITATION TANK(3,1)|RECYCLED BRINE SOLUTION(3,1)|SILICA RICH RESIDUE(3,1)|SPECIES PURIFICATION(3,1)|SYNTHETIC BRUCITE PRODUCTION(3,1)|PROCESS INTEGRATION(2,10)|NACL(2,3)|PH ADJUSTMENT(2,3)|3NA2SO(2,2)|CARBON DIOXIDE GAS SCRUBBING(2,2)|CARBON ISOLATION(2,2)|CRUSHING(2,2)|DEPLETION SOLUTION(2,2)|HCL SOLUTION(2,2)|MAGNESIUM HYDROXIDE PRECIPITATE PRODUCT(2,2)|NEUTRALIZING(2,2)|NI CO PRECIPITATION(2,2)|PRECIPITATE PRODUCTION(2,2)|SILICATE MINERAL(2,2)|SOFTENING(2,2)|ABSORBENT(2,1)|ACID LEACHANT(2,1)|ACID LEACHING CHEMISTRY(2,1)|ACIDIC REAGENT(2,1)|ADDED NAOHNEUTRALIZE EXCESS(2,1)|ADDRESSING(2,1)|ALKALI REAGENT(2,1)|ALKALI SPECIES(2,1)|ALKALIZATION(2,1)|ALUMINUM CONTENT(2,1)|APPROXIMATION(2,1)|ARTIFICIAL CLIMATIC CHANGE(2,1)|BARREN SOLUTION(2,1)|CA DEPLETED SOLUTION(2,1)|CA DEPLETING SOLUTION(2,1)|CALCINATION(2,1)|CEMENT PRODUCTION CARBON STRENGTH(2,1)|CO 2WHILE(2,1)|COCL2 SALT(2,1)|DECARBONIZATION(2,1)|ELECTROLYSIS CHLORINE GAS PRODUCT(2,1)|ENHANCE PRECIPITATION(2,1)|ENTRAPPING AIR(2,1)|EXEMPLIFIED SODIUM PERSULFATE(2,1)|FE AL NEUTRALIZATION(2,1)|FERROUS REMOVAL(2,1)|GASEOUS CARBON DIOXIDE ISOLATION(2,1)|GROUND ORE(2,1)|ION EXCHANGE ELUENT(2,1)|IRON PRECIPITATION PRODUCT(2,1)|IRON RESIDUE(2,1)|KINETICS(2,1)|LEACHING SOLUTION(2,1)|LOW CARBON STEEL PRODUCTION(2,1)|MAGNESIUM HYDROXIDE PRECIPITATION(2,1)|MAGNETIC SEPARATOR(2,1)|METAL CARBONATE PRECIPITANT(2,1)|MG HYDROXIDE(2,1)|MINERAL DEGRADATION PRODUCT RELEASE(2,1)|PERFORMANCE CONCRETE(2,1)|PURIFIED NICKEL(2,1)|REDISSOLVE NI CO(2,1)|REFRACTORY MARKET PRODUCT(2,1)|SALT CLEAVAGE(2,1)|SOLUTION NICL2(2,1)|STAGE PRECIPITATE(2,1)|SULFATE SALT(2,1)|WEAKLY ACIDIC SOLUTION(2,1)||(CA3198500)|ALKALI HYDROXIDE PRECIPITANT(100,44)|BICARBONATE PRECIPITANT(85,37)|COMMINUTED MINERAL FEEDSTOCK(81,14)|HYDROXIDE PRECIPITANT(80,44)|PRECIPITATING IRON(55,16)|FE AI DEPLETED SOLUTION(42,16)|ACID LEACHANT(41,20)|PROCESSING COMMINUTED MINERAL FEEDSTOCK(39,4)|UNFAVORABLE KINETICS(39,1)|ALKALI HYDROXIDE PRODUCT(36,18)|PRECIPITATING NA2CO3 HYDRATE(34,2)|SOLID SILICEOUS RESIDUE(33,11)|PRECIPITATING NICKEL(33,4)|SOLID SILICEOUS RESIDUE ALKALIZATION(32,4)|MAGNESIUM PRECIPITATION(31,6)|HYDROXIDE PRODUCT(29,18)|IRON ALKALIZATION(28,4)|ALKALI METAL CARBONATE(27,51)|NICKEL SAPROLITE ORE(27,3)|ELECTROLYSIS(26,12)|HEMATITE PRODUCT PRECIPITATION(26,4)|AMORPHOUS SILICATE(22,3)|CARBON INTENSIVE NICKEL(22,2)|MG DEPLETED SOLUTION(21,18)|MARKETABLE PRODUCT(20,1)|CO2(19,41)|PRECIPITANT(19,15)|ASBESTOS ORE(19,3)|OLIVINE ORE(19,3)|MAFIC MINERAL(19,2)|SOLID NA2CO3 CRYSTALIZER PRODUCT(18,6)|COBALT(17,12)|PRECIPITATION(17,8)|PURIFIED NICKEL PRODUCT(17,4)|PRECIPITATING CALCIUM(17,2)|BASALT IC SAND MATERIAL(17,1)|ALKALI METAL(16,54)|HYDROMETALLURGICAL VALUE EXTRACTION(16,14)|SCRUBBING SOLUTION(16,9)|HEMATITE SEED MATERIAL(16,7)|COBALT HYDROXIDE PRECIPITATE(16,1)|TAILING(15,7)|COMMINUTING(15,6)|OLIVINE(15,5)|ELUANT(15,4)|MAGNESIUM CARBONATE PRECIPITATE PRODUCT(15,3)|ELECTROLYTIC GENERATION(15,2)|MGDEPLETED SOLUTION(15,1)|COBALT CARBONATE(14,7)|ALUMINUM HYDROXIDE(13,15)|MAGNESIUM HYDROXIDE(13,12)|MANGANESE(13,7)|ION EXCHANGE MEDIUM(13,4)|FE AL(12,23)|NI CO(12,21)|ION EXCHANGE(12,12)|MANGANESE HYDROXIDE(12,6)|LEACHING METAL(12,4)|SEQUESTERING CARBON DIOXIDE(12,2)|INORGANIC CHEMISTRY(12,1)|CARBON DIOXIDE(11,33)|CARBON DIOXIDE CAPTURE(11,11)|NI CO ION EXCHANGE(11,4)|SCRUBBING CARBON DIOXIDE(10,5)|CRYSTALIZATION(10,4)|NICKEL VALUE(10,3)|WOLLASTONITE(10,3)|ULTRAMAFIC ROCK(10,2)|CALCIUM HYDROXIDE PRODUCT(9,11)|OXIDANT(9,6)|ELECTROCHEMICAL(9,2)|MGCO3(8,12)|ELECTROLYTE SALT(8,6)|MIXED NI CO HYDROXIDE(8,2)|SALT SPLITTING(8,1)|3NA2SO(7,12)|CARBON DIOXIDE OFF GAS(7,8)|OFF GAS(7,8)|ALUMINUM PRECIPITATION(7,6)|CHLORALKALI ELECTROCHEMICAL(7,6)|SAPROLITE MATERIAL(7,2)|PCT IB(6,20)|CARBON SOURCE(6,8)|NA0C(6,5)|NAHCO3(6,4)|SODIUM HYPOCHLORITE(6,4)|NI CO MHP PRECIPITATION(6,3)|AMORPHOUS SILICA RESIDUE(6,2)|CRUSHED ORE FERROMAGNETIC CONTENT(6,1)|CEMENT MANUFACTURE(5,3)|MG PRECIPITATION(5,3)|CO2 ADDITION(5,2)|IRON PRECIPITATION(5,2)|MINERAL ACID(5,2)|MIXED HYDROXIDE PRECIPITATE(5,2)|ADSORBENT REGENERATION(5,1)|ALKALI REAGENT RECYCLING(5,1)|CARBON INTENSIVE AMORPHOUS SILICATE(5,1)|CARBON INTENSIVE NICKEL COPRODUCTION(5,1)|MGCO3 MINERALIZATION(5,1)|MGCO3 PRECIPITATION(5,1)|NA2CO3 PRECIPITANT(5,1)|NA2SO4 SALT SPLITTING(5,1)|PARTLY LEACHED ORE(5,1)|STAGE MHP PRECIPITATION(5,1)|STANDARD CHLORALKALI BRINE PRETREATMENT(5,1)|TRIVALENT CATION(5,1)|ULTRAMAFIC FEEDSTOCK(5,1)|5NA2SO(4,4)|ELECTROLYTIC REACTANT REGENERATION(4,2)|MANGANESE REMOVAL(4,2)|MN HYDROXIDE(4,2)|CARBON HEAVY PYROMETALLURGY(4,1)|CHLORALKALI PLANT(4,1)|CO2 MGCO3(4,1)|FE AI PRECIPITATION RESIDUE(4,1)|HCI LEACHING PRODUCT(4,1)|MANGANESE SCRUBBING(4,1)|MAXIMIZE OXIDATIVE REMOVAL(4,1)|MGCO3 RECOVERY(4,1)|PLURAL REFERENT(4,1)|POLISH FILTRATION(4,1)|PURITY MG DEPLETED BRINE(4,1)|REFRACTORY MARKET(4,1)|SILICEOUS RESIDUE(4,1)|UNTREATED MAFIC ROCK(4,1)|2H2SO(3,6)|H2O(3,5)|CRUSHING(3,3)|3NA2CO(3,2)|ALKALIZATION(3,2)|BASALTIC SAND MATERIAL(3,2)|CA DEPLETED SOLUTION(3,2)|CARBON DIOXIDE GAS SCRUBBING(3,2)|CO2 SCRUBBING(3,2)|CRYSTALIZER(3,2)|HCI SOLUTION(3,2)|IMPURITY(3,2)|IRON OXYHYDROXIDE(3,2)|IRON REMOVAL(3,2)|LEACHING TEMPERATURE(3,2)|MAGNESIUM HYDROXIDE PRECIPITATE PRODUCT(3,2)|NAOH SOLUTION(3,2)|NEUTRALIZING(3,2)|NI CO PRECIPITATION(3,2)|NI2SIO(3,2)|BRINE SATURATION EVAPORATION(3,1)|CHLOR ALKALI PLANT(3,1)|CO2 CONCENTRATED STREAM(3,1)|COARSE SEPARABLE PRECIPITATE(3,1)|CONCENTRATED CO2 STREAM(3,1)|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)|MAFIC SAND INPUT(3,1)|MAGNETIC BENEFICIATION(3,1)|MAGNETITE MANUFACTURE(3,1)|MAXIMIZE EXTRACTION(3,1)|MAXIMIZE PRECIPITATION(3,1)|MINERAL CARBONATE(3,1)|MINERAL SEED(3,1)|NICKEL COBALT PRECIPITATION(3,1)|PRECIPITATE FE AI(3,1)|PRECIPITATION TANK(3,1)|RECYCLED BRINE SOLUTION(3,1)|SEA ENVIRONMENT(3,1)|SEED RECYCLING(3,1)|SILICA RICH RESIDUE(3,1)|SPECIES PURIFICATION(3,1)|SYNTHETIC BRUCITE PRODUCTION(3,1)|TREATING NA2SO(3,1)|TREATING NACI(3,1)|HYDROMETALLURGICAL(2,11)|PROCESS INTEGRATION(2,11)|IRON HYDROXIDE(2,4)|KOH(2,4)|MGSO4(2,4)|NICL2(2,4)|SIO2(2,4)|GRINDING(2,3)|NISO4(2,3)|ACID LEACHING CHEMISTRY(2,1)|ACO SOLUTION(2,1)|ADDRESSING ANTHROPOGENIC CLIMATE CHANGE(2,1)|ALKALI METAL PRECIPITANT(2,1)|ALKALINE SPECIES(2,1)|ALUMINUM CONTENT(2,1)|APPROXIMATION(2,1)|BARREN SOLUTION(2,1)|CALCINATION(2,1)|CARBON INTENSIVE CONSTRUCTION(2,1)|CEMENT CARBON INTENSITY(2,1)|CO2 ENRICHED SOLUTION(2,1)|COCL2 SALT(2,1)|CONTAMINANT(2,1)|ELECTROLYSIS CHLORINE GAS PRODUCT(2,1)|ENHANCE PRECIPITATION(2,1)|FE AI PRECIPITATION PRODUCT(2,1)|FE AI PRECIPITATION TEMPERATURE(2,1)|FE AL NEUTRALIZATION(2,1)|HCI ACID LEACHING(2,1)|HCI PRODUCTION FACILITY(2,1)|HYDROMETALLURGICAL VALUE RECOVERY(2,1)|ION EXCHANGE ELUANT(2,1)|ION EXCHANGE SOFTENING(2,1)|IRON PRECIPITATE PRODUCTION(2,1)|IRON RESIDUE(2,1)|MAGNETIC SEPARATOR(2,1)|MAXIMIZE REMOVAL(2,1)|METAL CARBONATE PRECIPITANT(2,1)|MG CARBONATE(2,1)|MG HYDROXIDE(2,1)|MGCO3 FORMATION(2,1)|MGSIO RATIO(2,1)|MINERAL DISSOLUTION PRODUCT(2,1)|NAOH MANUFACTURE(2,1)|PERFORMANCE CONCRETE(2,1)|PH MODULATOR(2,1)|PURIFIED NICKEL(2,1)|STAGE PRECIPITATE(2,1)|STREAM CONCENTRATION(2,1)|SULFATE SALT(2,1)|TERMINAL ACIDITY(2,1)|TIRE MANUFACTURING INDUSTRY(2,1)|WEAKLY ACIDIC SOLUTION(2,1)| (US20240002973)|1. A process for processing a comminuted mineral feedstock, comprising:| a) leaching metal values from the comminuted mineral feedstock with an acid leachant, to produce a solid siliceous residue and a loaded leach solution;| b) precipitating iron and/or aluminum from the loaded leach solution with addition of:| a first alkali metal carbonate precipitant, to produce a carbon dioxide off gas, or,| a first alkali hydroxide precipitant,| to produce an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate product;| c) precipitating nickel and/or cobalt from the Fe/Al depleted solution or from a Ni/Co ion exchange eluant obtained from the Fe/Al depleted solution by selective extraction of nickel and/or cobalt on an ion exchange medium, wherein the precipitating is with addition of:| a second alkali metal carbonate or bicarbonate precipitant, or,| a second alkali hydroxide precipitant,| to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate or hydroxide precipitate product;| d) before or after step (c), precipitating iron and/or aluminum and/or manganese from the Ni/Co depleted solution with addition of an oxidant and with addition of:| a third alkali metal carbonate or bicarbonate precipitant, or,| a third alkali hydroxide precipitant,| to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product;| e) precipitating magnesium from the Fe/Al/Mn depleted solution with addition of:| a fourth alkali hydroxide precipitant, or| a fourth alkali metal carbonate or bicarbonate precipitant,| to produce a Mg-depleted solution and a magnesium hydroxide or carbonate precipitate product;| f) subjecting the Mg-depleted solution to an electrolysis process to produce the acid leachant and:| one or more of the alkali hydroxide precipitants, or| an alkali hydroxide product.|2. The process of claim 1, further comprising reacting the alkali hydroxide product of the electrolysis process directly or indirectly with a carbon source to produce one or more of the alkali metal carbonate or bicarbonate precipitants.|3. The process of claim 2, wherein reacting the alkali hydroxide product with a carbon source comprises scrubbing carbon dioxide from a CO2 containing gas by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide product, to produce one or more of the alkali metal carbonate or bicarbonate precipitants.|4. The process of claim 3, wherein the alkali hydroxide product comprises NaOH, wherein scrubbing carbon dioxide from the CO2 containing gas comprises precipitating Na2CO3 hydrates from the scrubbing solution in a crystallisation process to produce a solid Na2CO3 crystallizer product.|5. The process of any one of claims 1-4, further comprising precipitating calcium from the Mg-depleted solution with a fifth alkali hydroxide precipitant, to produce a calcium hydroxide product, and generating one or more of the alkali metal carbonate or bicarbonate precipitants by treating the calcium hydroxide product with a carbon source.|6. The process of claim 5, wherein the carbon source is a CO2 containing gas or a metal carbonate.|7. The process of claim 3, 4 or 6, wherein the CO2 containing gas comprises air.|8. The process of claim 4, wherein one or more of the alkali metal carbonate or bicarbonate precipitants comprises the solid Na2CO3 crystallizer product.|9. The process of any of claims 1-8, wherein the alkali metal carbonate or bicarbonate precipitant comprises NaHCO3, Na2CO3 or K2CO3.|10. The process of any one of claims 1-9, wherein the alkali hydroxide precipitant comprises NaOH or KOH.|11. The process of any one of claims 1-10, wherein the acid leachant comprises a mineral acid, HCl or H2SO4.|12. The process of any one of claims 1-11, wherein the electrolysis process comprises a chloralkali process producing the alkali hydroxide precipitant and/or the alkali hydroxide product, a Cl2(g) product and a H2(g) product, further comprising reacting the Cl2(g) product and the H2(g) product to produce HCl as the acid leachant.|13. The process of any one of claims 1-11, wherein the Mg-depleted solution comprises Na2SO4, wherein the electrolysis process comprises a salt splitting process comprising electrolytic generation of: the alkali hydroxide product and/or the alkali hydroxide precipitant; and, H2SO4 as the acid leachant.|14. The process of any one of claims 1-13, wherein precipitating magnesium from the Fe/Al/Mn depleted solution with the alkali hydroxide precipitant, further comprises addition of a CO2(g) precipitant to produce the Mg-depleted solution and the magnesium carbonate precipitate product.|15. The process of claim 14, wherein the CO2(g) precipitant comprises the carbon dioxide off gas from the step of precipitating iron and/or aluminum from the loaded leach solution.|16. The process of any one of claims 1-15, wherein the oxidant comprises chlorine gas (Cl2(g)) or sodium hypochlorite (NaOCl).|17. The process of any one of claims 1-16, wherein the nickel and/or cobalt hydroxide precipitate is a mixed Ni/Co hydroxide product.|18. The process of any one of claims 1-17, further comprising magnetically separating material from the comminuted mineral feedstock.|19. The process of any one of claims 1-18, further comprising subjecting the loaded leach solution to a resin in leach process so as to selectively remove nickel values from the loaded leach solution, to obtain a purified nickel product.|20. The process of any one of claims 1-19, further comprising washing and/or alkalization of the solid siliceous residue.|21. The process of any one of claims 1-20, further comprising washing and/or alkalization of the iron and/or aluminum hydroxide or oxide precipitate product.|22. The process of any one of claims 1-21, further comprising adding a hematite seed material to the step of precipitating iron and/or aluminum so as to seed the precipitation of a hematite product.|23. The process of any one of claims 1-21, wherein the iron and/or aluminum hydroxide or oxide precipitate product comprises a hematite seed material, and the hematite seed material is recirculated to the step of precipitating iron and/or aluminum so as to seed the precipitation of a hematite product.|24. The process of any one of claims 1-23, further comprising recycling a brine comprising the Fe/Al/Mn depleted solution to a comminuting step to provide the comminuted mineral feedstock.|25. The process of any one of claims 1-24, wherein the mineral feedstock comprises a nickel saprolite ore or tailing, an olivine ore or tailing, an asbestos ore or tailing, a mafic mineral, a saprolite material, an ultramafic rock, olivine or wollastonite.|25. A process for processing a comminuted mineral feedstock, comprising:| optionally magnetically separating material from the comminuted mineral feedstock;| a) leaching metal values from the comminuted mineral feedstock with an acid leachant, to produce a solid siliceous residue and a loaded leach solution;| optionally subjecting the loaded leach solution to a resin in leach process so as to selectively remove nickel values from the loaded leach solution, to obtain a purified nickel product,| optionally, washing and/or alkalization of the solid siliceous residue;| b) precipitating iron and/or aluminum from the loaded leach solution with addition of:| a first alkali metal carbonate or bicarbonate precipitant,| to produce a carbon dioxide off gas, or,| a first alkali hydroxide precipitant,| to produce an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate product, optionally a hematite product;| optionally, washing and/or alkalization of the iron and/or aluminum hydroxide precipitate product;| optionally, adding a hematite seed material to the step of precipitating iron and/or aluminum, and further optionally wherein the iron and/or aluminum hydroxide or oxide precipitate product comprises the hematite seed material;| c) precipitating nickel and/or cobalt from the Fe/Al depleted solution or from a Ni/Co ion exchange eluant obtained from the Fe/Al depleted solution by selective extraction of Ni and/or cobalt on an ion exchange medium, wherein the precipitating is with addition of:| a second alkali metal carbonate or bicarbonate precipitant, or,| a second alkali hydroxide precipitant,| to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate or hydroxide precipitate product;| d) before or after step (c), precipitating iron and/or aluminum and/or manganese from the Ni/Co depleted solution with addition of an oxidant and with addition of:| a third alkali metal carbonate or bicarbonate precipitant, or,| a third alkali hydroxide precipitant,| to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product;| optionally recycling a brine comprising the Fe/Al/Mn depleted solution to a comminuting step to provide the comminuted mineral feedstock;| e) precipitating magnesium from the Fe/Al/Mn depleted solution with addition of:| a fourth alkali hydroxide precipitant, or| a fourth alkali metal carbonate or bicarbonate precipitant,| to produce a Mg-depleted solution and a magnesium hydroxide or carbonate precipitate product;| f) subjecting the Mg-depleted solution to an electrolysis process to produce the acid leachant and:| one or more of the alkali hydroxide precipitants, or| an alkali hydroxide product; and,| g) sequestering carbon dioxide from a CO2 containing gas, by reacting the CO2 containing gas directly or indirectly with the alkali hydroxide product, in one or more of: the nickel and/or cobalt carbonate precipitate product; or, the magnesium carbonate precipitate product. (US20240002973)|FIELD|[0001] The invention is in the field of inorganic chemistry, integrating electrochemical processes with steps of hydrometallurgical value extraction and carbon dioxide capture.|BACKGROUND|[0002] Technologies for efficient sequestration of gaseous carbon dioxide are potentially an important tool for addressing anthropogenic climate change. Various approaches have been suggested for sequestering carbon as mineral carbonates, including techniques that accelerate weathering reactions of minerals in ultramafic and mafic source rocks. These enhanced weathering (on land) or ocean alkalinity enhancement (at sea) approaches consume CO2 but are necessarily accompanied by a release of mineral dissolution products such as alkaline species and metal compounds, for example Si, Ca, Mg, Fe, Ni, and Co species. The ecological effect of these processes are uncertain (see Bach et al., CO2 Removal With Enhanced Weathering and Ocean Alkalinity Enhancement: Potential Risks and Co-benefits for Marine Pelagic Ecosystems, Frontiers in Climate, vol. 1, 2019, pg 7). There is a need for processes that integrate carbon capture with the recovery of metal values from mineral feedstocks.|SUMMARY|[0003] Processes are provided in which successive steps of hydrometallurgical value extraction are carried out on a mineral feedstock, such as an olivine, mafic, saprolite or ultramafic feedstock. In select embodiments, the products of carbon capture reactions and an electrolytic reagent-generating process are utilized as inputs to hydrometallurgical value recovery steps. The electrolytic process provides the acid leachant (HCl or H2SO4) and an alkali hydroxide (NaOH or KOH), with the alkali hydroxide then available for use either directly as a precipitant in the hydrometallurgical steps, or available for conversion to an alkali metal carbonate or bicarbonate that can in turn be used as the precipitant in the hydrometallurgical steps. In an alternative embodiment, the alkali hydroxide from the chloralkali process may be used to precipitate a calcium hydroxide product, with the calcium hydroxide product then available for use directly in carbon dioxide gas scrubbing, or for use to accept a carbonate that is provided by a CO2 scrubbing process.|[0004] Processes are accordingly provided for the coproduction from mineral feedstocks such as basaltic rocks of less carbon intensive, or carbon negative, nickel, iron, calcium and magnesium hydroxides or carbonates. Basaltic sand materials that include amorphous silicates may also be produced. These processes may involve (1) magnetic separation, (2) hydrochloric or sulfuric acid leaching, (3) selective precipitation of metal hydroxides or carbonates in successive steps, which may involve pH modulation (in select embodiments, nickel may for example be separated using a resin in leach step) (4) electrolysis of a resulting barren solution, for example a chloralkali process for treating NaCl(aq), or an electrolytic salt splitting anion exchange process for treating Na2SO4(aq), and (5) acid and alkali reagent recycling, for example in the case of a chloralkali process, hydrochloric acid production from the hydrogen and chlorine gas products of the electrolysis.|[0005] Process of the invention accordingly provide for the use of less carbon intensive nickel, iron, calcium and magnesium hydroxides or carbonates, as well as olivine and basaltic sand material, including amorphous silicates, in marketable products. These may for example include feedstocks for battery, steel, cement, tyre, glass, aggregate, or concrete industries. Products of the present processes, such as the solid siliceous residue or iron precipitate products, may for example be subject to washing and/or alkalization. The adjustment of pH by way of alkalization (alkali addition) may improve the suitability of the final product, for example to produce a siliceous residue suitable for use as a supplementary cementitious material (SCM) in cements with improved cementitious properties.|[0006] The present processes provide avenues for the coproduction of less carbon intensive nickel and iron hydroxides, and this in turn may provide avenues to decarbonate sectors associated with the transition to a low carbon economy—such as electric vehicles and batteries. The invention also facilitates low carbon steelmaking, by compensating carbon heavy pyrometallurgy with a carbon negative magnetic, hydrometallurgical and electrochemical process.|[0007] The present processes provide for the coproduction of less carbon intensive amorphous silicates, marketable as a supplementary cementitious material (SCM) for cements, or in the tyre manufacturing industry. Basaltic sand materials may be produced by the present processes, with an inert surface, for example for use as aggregate in concrete mixes. The invention accordingly facilitates the construction of less carbon intensive concrete buildings.|[0008] Processes are accordingly provided for processing a comminuted mineral feedstock, comprising:| - optionally magnetically separating material from the comminuted mineral feedstock;| - a) leaching metal values from the comminuted mineral feedstock with an acid leachant, to produce a solid siliceous residue and a loaded leach solution;| - optionally subjecting the loaded leach solution to a resin in leach process so as to selectively remove nickel and cobalt values from the loaded leach solution, to obtain a purified nickel and cobalt combined product,| - optionally, washing and/or alkalization of the solid siliceous residue, for example to form a supplementary cementitious material (SCM) for use in cements;| - b) precipitating iron and/or aluminum from the loaded leach solution with addition of: | - a first alkali metal carbonate or bicarbonate precipitant,| - to produce a carbon dioxide off gas, or, | - a first alkali hydroxide precipitant,| - to produce an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide (e.g. hematite) precipitate product;| - optionally, washing and/or alkalization of the iron and/or aluminum hydroxide precipitate product;| - optionally, adding a hematite seed material to the step of precipitating iron and/or aluminum, wherein the iron and/or aluminum hydroxide precipitate product may comprise the hematite seed material, which is then recirculated to the precipitation step;| - c) precipitating nickel and/or cobalt from the Fe/Al depleted solution or from a Ni/Co ion exchange eluant obtained from the Fe/Al depleted solution by selective extraction of Ni and/or cobalt on an ion exchange medium, wherein the precipitating is with addition of: | - a second alkali metal carbonate or alkali metal bicarbonate precipitant, or,| - a second alkali hydroxide precipitant,| - to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate or hydroxide precipitate product;| - d) before or after step (c), precipitating iron and/or aluminum and/or manganese from the Ni/Co depleted solution with addition of an oxidant and with addition of: | - a third alkali metal carbonate or bicarbonate precipitant, or,| - a third alkali hydroxide precipitant,| - to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product;| - optionally recycling a brine comprising the Fe/Al/Mn depleted solution to a comminuting step to provide the comminuted mineral feedstock;| - e) precipitating magnesium from the Fe/Al/Mn depleted solution with addition of: | - a fourth alkali hydroxide precipitant, or| - a fourth alkali metal carbonate or bicarbonate precipitant,| - to produce a Mg-depleted solution and a magnesium hydroxide or carbonate precipitate product;| - f) subjecting the Mg-depleted solution to an electrolysis process to produce the acid leachant and: | - one or more of the alkali hydroxide precipitants, or| - an alkali hydroxide product, available for conversion into one or more of the alkali metal carbonate or bicarbonate precipitants; and,| - g) optionally sequestering carbon dioxide from a CO2 containing gas, for example by reaction with the alkali hydroxide product, and/or in one or more of: the nickel and/or cobalt carbonate precipitate product; or, the magnesium hydroxide precipitate product.|[0037] Processes may further include scrubbing carbon dioxide from a CO2 containing gas, including ambient air, by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide precipitant, to produce one or more of the alkali metal carbonate or bicarbonate precipitants.|[0038] Processes are according provided for processing a comminuted mineral feedstock, comprising:| - a) leaching metal values from the comminuted mineral feedstock with an acid leachant, to produce a solid siliceous residue and a loaded leach solution;| - b) precipitating iron and/or aluminum from the loaded leach solution with addition of: | - a first alkali metal carbonate precipitant, to produce a carbon dioxide off gas, or,| - a first alkali hydroxide precipitant,| - to produce an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate (such as hematite) product;| - c) precipitating nickel and/or cobalt from the Fe/Al depleted solution or from a Ni/Co ion exchange eluant obtained from the Fe/Al depleted solution by selective extraction of nickel and/or cobalt on an ion exchange medium, wherein the precipitating is with addition of: | - a second alkali metal carbonate or bicarbonate precipitant, or,| - a second alkali hydroxide precipitant,| - to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate or hydroxide precipitate product, such as a mixed Ni/Co hydroxide product;| - d) before or after step (c), precipitating iron and/or aluminum and/or manganese from the Ni/Co depleted solution with addition of an oxidant (such as chlorine gas (Cl2(g)) or sodium hypochlorite (NaOCL)) and with addition of: | - a third alkali metal carbonate or bicarbonate precipitant, or,| - a third alkali hydroxide precipitant,| - to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product;| - e) precipitating magnesium from the Fe/Al/Mn depleted solution with addition of: | - a fourth alkali hydroxide precipitant, or| - a fourth alkali metal carbonate or bicarbonate precipitant,| - to produce a Mg-depleted solution and a magnesium hydroxide or carbonate precipitate product;| - f) subjecting the Mg-depleted solution to an electrolysis process to produce the acid leachant and: | - one or more of the alkali hydroxide precipitants, or| - an alkali hydroxide product.|[0059] Processes may further involve reacting the alkali hydroxide product of the electrolysis process directly or indirectly with a carbon source to produce one or more of the alkali metal carbonate or bicarbonate precipitants. The step of reacting the alkali hydroxide product with a carbon source may involve scrubbing carbon dioxide from a CO2 containing gas by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide product, to produce one or more of the alkali metal carbonate or bicarbonate precipitants.|[0060] In select embodiments, calcium may be precipitated from the Mg-depleted solution with a fifth alkali hydroxide precipitant, to produce a calcium hydroxide product, and generating one or more of the alkali metal carbonate or bicarbonate precipitants by treating the calcium hydroxide product with a carbon source, such as a CO2 containing gas or a metal carbonate, and the CO2 containing gas may for example be air. When the alkali hydroxide product comprises NaOH, scrubbing carbon dioxide from the CO2 containing gas may accordingly involve precipitating Na2CO3 hydrates from the scrubbing solution in a crystallisation process to produce a solid Na2CO3 crystallizer product, and one or more of the alkali metal carbonate or bicarbonate precipitants comprises the solid Na2CO3 crystallizer product.|[0061] In alternative embodiments, the alkali metal carbonate or bicarbonate precipitant may be one or more of NaHCO3, Na2CO3 or K2CO3, or a mixture thereof. The alkali hydroxide precipitant may be one or both of NaOH or KOH, or a mixture thereof. The acid leachant may for example be a mineral acid, such as HCl or H2SO4, or a mixture thereof.|[0062] The electrolysis process may involve a chloralkali process, producing the alkali hydroxide precipitant and/or the alkali hydroxide product, a Cl2(g) product and a H2(g) product. The Cl2(g) product and the H2(g) product may then be reacted to produce HCl as the acid leachant.|[0063] When the Mg-depleted solution includes Na2SO4, the electrolysis process may involve a salt splitting process that includes electrolytic generation of: the alkali hydroxide product and/or the alkali hydroxide precipitant; and, H2SO4 as the acid leachant.|[0064] Precipitating magnesium from the Fe/Al/Mn depleted solution with the alkali hydroxide precipitant, may involve addition of a CO2(g) precipitant to produce the Mg-depleted solution and the magnesium carbonate precipitate product. The CO2(g) precipitant may for example include, or be made entirely from, the carbon dioxide off gas from the step of precipitating iron and/or aluminum from the loaded leach solution.|[0065] In select embodiments, an initial step of magnetically separating material from the comminuted mineral feedstock may be implements, for example so as to enrich the feedstock in select materials.|[0066] In select embodiments, the loaded leach solution may be subjected to a resin in leach process so as to selectively remove nickel values from the loaded leach solution, to obtain a purified nickel product.|[0067] The products of the process may be further treated for example by washing and/or alkalization of the solid siliceous residue, washing and/or alkalization of the iron and/or aluminum hydroxide or oxide precipitate product.|[0068] A hematite seed material may be added to the step of precipitating iron and/or aluminum so as to seed the precipitation of a hematite product. When the iron and/or aluminum hydroxide or oxide precipitate product comprises a hematite seed material, the hematite seed material may be recirculated to the step of precipitating iron and/or aluminum so as to seed the precipitation of a hematite product.|[0069] A brine that includes some or all of the Fe/Al/Mn depleted solution may be recirculated to the comminuting step, to provide the comminuted mineral feedstock.|[0070] The mineral feedstock may for example be, or include, one or more of a nickel saprolite ore or tailing, an olivine ore or tailing, an asbestos ore or tailing, a mafic mineral, a saprolite material, an ultramafic rock, olivine, wollastonite or combinations thereof.|(US20240002973)|BRIEF DESCRIPTION OF THE DRAWINGS|[0071] FIG. 1 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process.|[0072] FIG. 2 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process.|[0073] FIG. 3 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process.|[0074] FIG. 4 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process.|[0075] FIG. 5 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process, showing the use of Na2CO3 to precipitate Mg.|[0076] FIG. 6 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process, showing the use of NaOH in combination with CO2(g) to precipitate Mg.|[0077] FIG. 7 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by an electrolytic salt splitting anion exchange process.|[0078] FIG. 8 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide (DAC) and an electrolytic salt splitting anion exchange process.|[0079] FIG. 9 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide (DAC) and an electrolytic salt splitting anion exchange process.|[0080] FIG. 10 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide (DAC) and an electrolytic salt splitting anion exchange process.|[0081] FIG. 11 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, which includes an initial step of magnetic beneficiation to adjust the metal content of the treated material.|(US20240002973)|DETAILED DESCRIPTION|[0082] Processes are provided in which successive steps of hydrometallurgical value extraction are carried out using the products of carbon capture and an electrolytic reactant regeneration process, such as a chloralkali process or an electrolytic salt splitting anion exchange process. The electrolytic reactant regeneration process provides an acid leachant and an alkali hydroxide, with the alkali hydroxide (e.g. NaOH) then available for use either directly as a precipitant in the hydrometallurgical steps, or available for conversion to an alkali metal carbonate (e.g. Na2CO3) or bicarbonate (e.g. NaHCO3) that can in turn be used as the precipitant in the hydrometallurgical steps.|[0083] In an alternative embodiment, the alkali hydroxide from the chloralkali process may be used to precipitate a calcium hydroxide product, with the calcium hydroxide product then available for use directly in carbon dioxide gas scrubbing, or for use to accept a carbonate that is provided by a CO2 scrubbing process.|[0084] In some embodiments, a crystalliser step may be introduced to precipitate Na2CO3 or Na2CO3 hydrates from a CO2 enriched solution that is being treated with the alkali hydroxide (NaOH) product of the chloralkali process. In such processes, a crystalliser may be used to reduce water content in the hydrates by modulating temperature, pressure and NaOH concentration. The solid Na2CO3 product may then be used as a carbonate precipitant.|[0085] By using a carbonate precipitant to precipitate iron and aluminum from the leach solution, at a suitably low pH, the carbonate will decompose to release a concentrated stream of CO2, and the concentrated CO2 stream may in turn be sequestered or fixed.|[0086] FIG. 1 illustrates a process in which metal values are leached from a comminuted (“crushing and grinding”) mineral feedstock with an acid leachant (“HCl leaching”), to produce a solid siliceous residue (“Amorphous Silica Residue for Cement Manufacture”) and a loaded leach solution. As illustrated, the residue may be washed. Crushing and grinding in a recycled brine solution containing a variety of chloride or sulfate salts, such as magnesium and sodium salts, may be carried out so as to avoid or minimize the need for the addition of non-brine water. HCl acid leaching may be carried out at relatively high acid concentrations, such as 30-36% HCl by weight in water—a typical product from an HCl production facility attached to a chlor-alkali plant.|[0087] As illustrated in FIG. 11, in an embodiment of the invention, the ferromagnetic content of the crushed ore may be modulated using a magnetic separator, for example so as to increase or decrease the iron and nickel hydroxide products of the process. For example, with an (ultra)mafic sand input comprising olivine or wollastonite, the ratio of MgSiO4 and CaSiO4 content to nickel and iron may be optimised via magnetic separation. In a further alternative, a resin in leach process may be used to selectively remove nickel content in the acidic leach prior to selective precipitation steps, to obtain a purified nickel product.|[0088] Conditions for leaching may include a leaching temperature of from 80° C. to boiling point, to 115° C. or higher. Acid addition during HCl leaching may for example range from 500 to 1000 kg HCl per dry tonne of solid feed, varying with the chemical composition of the feed. Leaching times may for example be for effective residence times of from 1 hour to 8 hours. Leaching may for example be carried out in a single stage or two or more countercurrent stages. In a single stage process, the acid and ore are added together and allowed to react at a leaching temperature to completion. In a multistage leach, fresh ore is contacted with partly reacted solution so as to maximize the use of the acid (low terminal acidity) and in the second or subsequent stage, the partly leached ore (from the first stage) is contacted with high acid to maximize extraction of Mg/Ni/Co/Fe, etc. The multistage process may involve additional solid/liquid separation steps to ensure countercurrent movement of solids and liquids.|[0089] The raw materials for the present processes may contain a variety of silicate minerals including magnesium, iron, nickel and cobalt and minor impurity elements. The chemistry of acid leaching, with HCl, may therefore be represented the following reactions:|Mg2SiO4+4HCl=2MgCl2+SiO2+2H2O|Ni2SiO4+4HCl=2NiCl2+SiO2+2H2O|Fe2SiO4+4HCl=2FeCl2+SiO2+2H2O|[0090] Other minerals present in source materials such as iron oxides or aluminum oxides may also react with HCl to form additional salts in solution:|FeO(OH)+3HCl=FeCl3+2H2O|AlO(OH)+3HCl=AlCl3+2H2O|[0091] Natural mineral source materials are of course not pure compounds, so that the source minerals my contain a variety of elements (eg. Mg, Ni, Co, Fe in one silicate mineral) and may be hydrated or weathered. Geological descriptions of suitable feed materials include: nickel saprolite ores, olivine ores, and asbestos ores and tailings.|[0092] The product of HCl leaching is a weakly acidic solution containing various chloride salts. A silica rich residue is recovered as a solid product. This residue may for example be washed to remove salts and excess acid with fresh water, and/or alkalized (alkali conditioning) with a base to adjust pH, and then directed to cement manufacture where the silica may be used as a replacement for other materials (thus lowering the carbon intensity of cement manufacture) and as a strengthener to improve the yield strength of concrete, with the silica acting as a supplementary cementitious material (SCM) in a high performance concrete.|[0093] Iron and/or aluminum are precipitated (“Iron and Aluminum Precipitation”) from the loaded leach solution with an alkali hydroxide (NaOH) or alkali metal carbonate or bicarbonate precipitant (Na2CO3 as illustrated in FIG. 1). When Na2CO3 is used as a precipitant, this produces a carbon dioxide off gas (“CO2 Off Gas”), an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate product (“Fe/Al Hydroxide Precipitate” as illustrated, comprising magnetite in select embodiments). As illustrated, the residue is washed to provide the precipitate. When an alkali hydroxide (e.g. KOH or NaOH) is used as the precipitant, the iron and aluminum content in the solution is generally precipitated as a mix of oxide and hydroxide solids by raising the pH with an alkali hydroxide (KOH or NaOH) solution. The NaOH solution may for example be added as a 50% solution, and may be diluted with recycled brine solution for process convenience and enhanced pH control (it may be hard to control pH when adding a very strong base). The added NaOH neutralizes excess acid and precipitates Fe/Al and other trivalent cations if present:|HCl+NaOH=NaCl+H2O|FeCl3+3NaOH═FeO(OH)+3NaCl+H2O|2FeCl3+6NaOH═Fe2O3(hematite)+6NaCl+3H2O|AlCl3+3NaOH═AlO(OH)+3NaCl+H2O|2AlCl3+6NaOH=Al2O3+6NaCl+3H2O|CrCl3+3NaOH═CrO(OH)+3NaCl+H2O|2CrCl3+6NaOH=Cr2O3+6NaCl+3H2O|[0094] The pH adjustment may for example be conducted with stoichiometric amounts of alkali hydroxide. Over-addition of NaOH may result in precipitation of Ni/Co (undesirable) so control of base addition must be maintained. The Fe/Al precipitation temperature may for example be 75° C. to boiling point. Seed (precipitate) may be recycled, for example in the form of hematite, to ensure growth of suitably sized particles, and materials, for enhanced solid/liquid separation. An initial mineral seed, such as hematite, may be used to initiate the process of precipitating a select material, such as hematite. Fe/Al precipitation time may for example be 1 to 8 hours. NaOH may for example be added progressively through precipitation tanks (continuous) so as to enhance precipitation of coarser/separable precipitates. The Fe/Al precipitation product may be separated by S/L separation and washed.|[0095] The Fe/Al precipitation residue may for example be treated to form commercial products, such as hematite. For example, drying and partial reduction may be used to form magnetite and a mixed Al/Cr oxide. The magnetite can be separated using magnetic separation and the Al/Cr oxide can be sold as a product for the refractory market.|[0096] Nickel and cobalt may be selectively recovered in a variety of ways. In an HCl based leaching process, Ni and Co will be present in solution as NiCl2 and CoCl2 salts, and these salts can be recovered by ion exchange, for example using a Dow M4195 resin to extract Ni and Co in a Na-form resin. The resin can then be stripped with HCl solution to form a strong, purified solution of Ni/Co chloride salts. The resin may then be treated with NaOH solution after acid stripping to return to the resin “loading” step.|[0097] In select embodiments, the recovery of Ni/Co is by way of a mixed hydroxide precipitate (MHP). This can be done directly from the solution coming from the iron precipitation step, or can be effected starting with the ion exchange eluant containing nickel and cobalt chloride. In these processes, a solution of sodium hydroxide is added to from the precipitates:|NiCl2+2NaOH═Ni(OH)2+2NaCl|CoCl2+2NaOH═Co(OH)2+2NaCl|[0098] Other metals may also precipitate with the Ni/Co in minor amounts. For example Mn, Fe (remaining iron in solution).|[0099] The selectivity of Ni/Co MHP precipitation can be enhanced by using two stage MHP precipitation, in which a second stage precipitate is recovered and recycled to the first stage or to the discharge from the main leaching step (where acid is present to redissolve the Ni/Co and other metals from the second stage leach).|[0100] The mixed hydroxide precipitate may be recovered by S/L separation and washing. A pressure filter may be used with a “squeeze” cycle to minimize the entrained moisture in the washed Ni/Co MHP cake prior to shipping.|[0101] The Ni/Co MHP precipitation may be carried out between 25-90° C. with a terminal pH in the range of 5-8. The addition of base can also be controlled by stoichiometry rather than, or in addition to, pH. The Ni/Co MHP precipitation time may for example be 1-8 hours. Seed recycling may be used to maximize particle size and minimize contamination. The Ni/Co MHP process (as in all steps) may be conducted continuously.|[0102] As illustrated in FIG. 1, in an alternative embodiment nickel and/or cobalt may be precipitated from the Fe/Al depleted solution with a second alkali metal carbonate or bicarbonate precipitant (Na2CO3 as illustrated), to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate precipitate product (“Ni/Co Carbonate (to battery manufacture)”).|[0103] Most of the iron and aluminum are removed from solution in the first iron removal step. Manganese is generally not removed from solution in either the initial iron control or the Ni/Co MHP precipitation steps. Accordingly, a second stage of iron precipitation may be implemented with increased pH so as to maximize the removal of iron with an oxidant added to oxidize Mn and Fe to facilitate more complete removal and purification of all species. Suitable oxidants include gaseous chlorine or sodium hypochlorite (NaOCl). Example reactions include:|2FeCl2+NaOCl+4NaOH═2FeO(OH)+5NaCl+H2O|MnCl2+NaOCl+2NaOH=MnO2+3NaCl+H2O|AlCl3+3NaOH═AlO(OH)+3NaCl+H2O|[0104] Conditions for iron and/or aluminum and/or manganese scrubbing may be designed to maximize precipitation of the impurity elements while minimizing formation of magnesium hydroxide. The oxidant (eg. NaOCl) may be added so as to achieve a suitably high oxidation/reduction potential (ORP) to maximize the oxidative removal of Fe/Mn. Scrubbing temperature may for example be 25° C. to the boiling point. As in other precipitation steps, seed recycle can be used to improve performance. Scrubbing time may for example be 1 to 8 hours.|[0105] Alternatively, as illustrated in FIG. 1, iron and/or aluminum and/or manganese may be scrubbed from the Ni/Co depleted solution with a third alkali metal carbonate or bicarbonate precipitant (also Na2CO3 as illustrated) and an oxidant, such as the illustrated sodium hypochlorite, to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product (“Fe/Al/Mn Hydroxide Precipitate”). As illustrated, brine comprising the Fe/Al/Mn depleted solution may be recycled to the comminuting step to provide the comminuted mineral feedstock.|[0106] Magnesium remaining in solution may be precipitated from the Fe/Al/Mn depleted solution with an alkali hydroxide precipitant (NaOH as illustrated), to produce a Mg-depleted solution and a magnesium hydroxide precipitate product (“Mg Hydroxide Precipitate”):|MgCl2+2NaOH═Mg(OH)2+2NaCl|[0107] This may for example be carried out by adding NaOH to MgCl2 solution, or by reversing the order of addition. In either case, the process may be carried out so as to provide a near complete removal of Mg as Mg(OH)2 from solution. This generally requires a near stoichiometric addition of NaOH.|[0108] The Mg-depleted solution may then be subjected to further purification, for example in an ion exchange resin separation step, or sent directly to an electrolysis to produce the alkali hydroxide precipitant and the acid leachant (in FIG. 1, “Chlor-Alkali Plant to make HCl and NaOH for Recycle”, in FIG. 7 “Salt Splitting Plant to make H2SO4 and NaOH for Recycle”). Standard chloralkali brine pretreatments may be carried out on the Mg-depleted solution to provide a higher purity Mg-depleted brine, for example essentially free of undesirable solids and ions, for example involving brine saturation/evaporation and softening, for example by primary and polish filtration steps and high-performance ion exchange softening. In an HCl based extraction process, the final Mg-depleted solution is NaCl(aq) with some minor contaminants in solution. This NaCl(aq) solution is directed to a chlor-alkali plant for manufacture of NaOH, Cl2 and H2, involving conventional steps, with the Cl2 and H2 available to be burned and water-scrubbed to form a strong HCl solution for recycle to leaching. Excess heat from Cl2 and H2 combustion may for example be recovered as steam and used to evaporate excess water from solution.|[0109] As illustrated in FIG. 1, carbon dioxide may be scrubbed from a CO2 containing gas (“Air” as illustrated) by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide precipitant (NaOH as illustrated), to produce one or more of the alkali metal carbonate or bicarbonate precipitants (Na2CO3 as illustrated).|[0110] In the foregoing process, the step of scrubbing carbon dioxide from the CO2 containing gas may include a crystallisation step to precipitate Na2CO3 hydrates from the scrubbing solution, the alkali hydroxide precipitant being NaOH. The solid Na2CO3 crystallizer product may then be directed to provide one or more of the alkali metal carbonate or bicarbonate precipitants.|[0111] FIG. 2 illustrates a process analogous to the process illustrated in FIG. 1, with potassium compounds in place of the sodium compounds of FIG. 1.|[0112] FIG. 3 and FIG. 4 illustrate alternative embodiments which involve precipitating calcium from the Mg-depleted solution with a fourth alkali metal hydroxide precipitant (NaOH as illustrated), to produce a Ca-depleted solution and a calcium hydroxide product. The calcium hydroxide product is then available for carbon sequestration reactions, for example by generating the metal carbonate precipitant for the iron and/or aluminum precipitation step by treating the calcium hydroxide product with a carbon source, such as air (FIG. 3) or a metal carbonate that is in turn derived from KOH-mediated carbon capture (FIG. 4). In these processes, the Ca-depleted solution is subjected to electrolysis to produce one or more of the first, second, third or fourth alkali metal hydroxide precipitants and the acid leachant.|[0113] The alkali hydroxide precipitant may accordingly be NaOH (FIGS. 1, 3 and 4) or KOH (FIG. 2). The process acid leachant as illustrated is HCl. These products may be produced in a chloralkali process.|[0114] FIG. 5 and FIG. 6 illustrate alternative embodiments, in which alternative pathways are used to form MgCO3 rather than Mg(OH)2 in the magnesium precipitation step. These embodiments reflect adaptations related to the use of Mg(OH)2 from the present processes for: (1) direct air capture (DAC) of CO2 to form MgCO3; or, (2) ocean alkalinity enhancement (OAE) to form Mg(HCO3)2 by direct addition of Mg(OH)2 to the ocean environment. The use of Mg(OH)2 to form MgCO3 by contact with air containing CO2 can in some circumstances suffer from unfavourable kinetics. The embodiments illustrated in FIG. 5 and FIG. 6 accordingly provide alternative routes to forming MgCO3 in approaches that may be adapted to optimize carbon sequestration.|[0115] FIG. 5 illustrates a process in which MgCO3 is formed by direct neutralization of the Fe/Al/Mn depleted solution, so that Na2CO3, for example produced in and recovered from a direct air capture (DAC) process, reacts with MgCl2 (aq) in the Fe/Al/Mn depleted solution to form MgCO3(s):|MgCl2+Na2CO3=MgCO3+2NaCl|[0116] In select embodiments, essentially the full amount of NaOH produced by the chloralkali process is directed to the DAC system to produce Na2CO3 from CO2 captured directly from the atmosphere. In such a process, sufficient Na2CO3 is produced to provide the alkali metal precipitant for all aspects of the process, including recovery of MgCO3. In this way, sorbent regeneration for DAC, i.e. NaOH, is combined with long term mineralisation of the CO2. MgCO3 mineralisation thereby creates carbon negative products in the form of carbonates, that may for example be used as filler or construction aggregate.|[0117] FIG. 6 illustrates an alternative process involving the formation of MgCO3 by direct addition of CO2 gas, with addition of NaOH, to the Fe/Al/Mn depleted solution, to react with MgCl2 (aq) in solution to form MgCO3(s):|MgCl2+2NaOH+CO2(g)=MgCO3+2NaCl+H2O|[0118] As illustrated in FIG. 6, a portion of NaOH from the chloralkali process may be directed to the Mg precipitation stage, together with CO2(g) (for example recovered as a CO2 off gas from iron and aluminum precipitation with Na2CO3), forming MgCO3 in-situ. Alternatively, CO2(g) for Mg carbonate precipitation may come from sources external to the present process.|[0119] Reactions in various stages of the present process may be represented as follows:|Neutralization| - Alkali hydroxide: 2HCl+2NaOH=2NaCl+2H2O| - Alkali metal carbonate: 2HCl+Na2CO3=2NaCl+H2O+CO2(g) |Iron Precipitation| - Alkali hydroxide: 2FeCl3+6NaOH═2FeO(OH)+2H2O+6NaCl | - 2FeCl3+6NaOH═Fe2O3 (hematite)+6NaCl+3H2O| - Alkali metal carbonate: 2FeCl3+3Na2CO3+H2O ═2FeO(OH)+6NaCl+3CO2(g) |Nickel Recovery| - Alkali hydroxide: NiCl2+2NaOH═Ni(OH)2+2NaCl| - Alkali metal carbonate: NiCl2+Na2CO3=NiCO3+2NaCl|Magnesium Recovery| - Alkali hydroxide: MgCl2+2NaOH═Mg(OH)2+2NaCl| - Alkali metal carbonate: MgCl2+Na2CO3=MgCO3+2NaCl| - Direct CO2: MgCl2+2NaOH+CO2(g)=MgCO3+2NaCl+H2O|[0130] In alternative embodiments, NaHCO3 may take the place of Na2CO3 in reactions in various stages of the present process.|[0131] FIGS. 7-10 illustrate processes in which metal values are leached from a comminuted (“crushing and grinding”) mineral feedstock with a sulfuric acid leachant (“H2SO4 leaching”), to produce a solid siliceous residue (“Amorphous Silica Residue for Cement Manufacture”) and a loaded leach solution. As illustrated, the residue may be washed.|[0132] Iron and/or aluminum are precipitated (“Iron and Aluminum Precipitation”) from the loaded leach solution with either an alkali hydroxide precipitant (FIG. 7) or an alkali metal carbonate or bicarbonate precipitant (Na2CO3 FIGS. 8-10). Use of the alkali metal carbonate or bicarbonate precipitant produces a carbon dioxide off gas (“CO2 Off Gas”), an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate product (“Fe/Al Hydroxide Precipitate”, which may be an oxide, such as hematite). The concentrated CO2 Off Gas may be sequestered using a variety of approaches. As illustrated, the residue may be washed to provide the precipitate, and the precipitate may be used in magnetite manufacture.|[0133] Nickel and/or cobalt are precipitated from the Fe/Al depleted solution with the alkali hydroxide precipitant (e.g. NaOH, FIG. 7) or the alkali metal carbonate or bicarbonate precipitant (e.g. Na2CO3, FIGS. 8-10), to produce a Ni/Co depleted solution and a nickel and/or cobalt hydroxide (FIG. 1, “MHP”) or carbonate precipitate product (FIGS. 8-10, “Ni/Co Carbonate (to battery manufacture)”).|[0134] Iron and/or aluminum and/or manganese may be scrubbed from the Ni/Co depleted solution with the alkali hydroxide precipitant (FIG. 7) or with the alkali metal carbonate or bicarbonate precipitant (FIGS. 8-10, Na2CO3) and an oxidant, such as the illustrated sodium persulfate (Na2S2O8), to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product (“Fe/Al/Mn Hydroxide Precipitate”).|[0135] As illustrated, brine comprising the Fe/Al/Mn depleted solution may be recycled to the comminuting step to provide the comminuted mineral feedstock.|[0136] Magnesium may be precipitated from the Fe/Al/Mn depleted solution with the alkali hydroxide precipitant (NaOH as illustrated in FIGS. 7 and 8), or with the alkali metal carbonate or bicarbonate precipitant (FIG. 9) or with a combined feed of the alkali hydroxide precipitant and CO2 (in a carbon dioxide capture step,|[0137] FIG. 10) to produce a Mg-depleted solution and a magnesium hydroxide (FIGS. 7 and 8) or carbonate (FIGS. 9 and 10) precipitate product, The Mg-depleted solution may then be subjected to an electrolysis to produce the alkali hydroxide precipitant and the acid leachant (“Salt Splitting Plant to make H2SO4 and NaOH for Recycle”).|[0138] Carbon dioxide may be scrubbed from a CO2 containing gas (“Air” as illustrated) by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide precipitant (NaOH as illustrated), to produce one or more of the first, second, third and fourth alkali metal carbonate or bicarbonate precipitants (Na2CO3 as illustrated), for use respectively in i) iron and aluminum precipitation, ii) Ni/Co precipitation, iii) iron and aluminum precipitation with manganese removal, and iv) Mg precipitation.|[0139] In the foregoing process, the step of scrubbing carbon dioxide from the CO2 containing gas may include a crystallisation step to precipitate Na2CO3 hydrates from the scrubbing solution, the alkali hydroxide precipitant being NaOH. The solid Na2CO3 crystalizer product may then be directed to provide one or more of the alkali metal carbonate or bicarbonate precipitants.|[0140] The process acid leachant as illustrated is H2SO4. As such, processes are provided that use of a sulfate based system for treatment of magnesium silicates. In select embodiments, (FIG. 7) H2SO4/NaOH/Na2SO4 salt splitting is used to produce amorphous silica for cementing, iron residue, mixed nickel and cobalt hydroxide and magnesium hydroxide—which is then available for carbon sequestration. In alternative embodiments, various direct air carbon capture (DAC) steps are integrated into the sulfate system (FIGS. 8-10). In particular, FIG. 8 illustrates a process wherein a portion of the alkali hydroxide precipitant NaOH is used to remove CO2 from air. The resulting sodium carbonate is then used in the iron removal and the nickel/cobalt precipitation stages. FIG. 9 illustrates a process in which there is complete use of NaOH for DAC to form Na2CO3. The addition of Na2CO3 to the Mg precipitation stage results in MgCO3 precipitation directly for carbon sequestration. FIG. 10 illustrates an alternative embodiment in which the alkali hydroxide precipitant NaOH is combined with CO2 added directly to the Mg precipitation stage, to form MgCO3.|[0141] Steps in the sulfate process may be characterized by reactions therein, as follows:|Acid leaching (simplified);| - Mg2SiO4+2H2SO4=2MgSO4+SiO2+2H2O| - Ni2SiO4+2H2SO4=2NiSO4+SiO2+2H2O| - Co2SiO4+2H2SO4=2CoSO4+SiO2+2H2O| - Fe2SiO4+2H2SO4=2FeSO4+SiO2+2H2O| - MnO2+2FeSO4+2H2SO4=MnSO4+Fe2(SO4)3+2H2O| - 2FeO(OH)+3H2SO4═Fe2(SO4)3+4H2O| - 2Al(OH)+3H2SO4═Al2(SO4)3+4H2O|Iron/aluminum removal (with product);| - H2SO4+2NaOH=Na2SO4+2H2O| - Al2(SO4)3+6NaOH═2Al(OH)3+3Na2SO4 (Aluminum hydroxide)| - Fe2(SO4)3+6NaOH═2Fe(OH)3+3Na2SO4 (Iron hydroxide)| - Al2(SO4)3+6NaOH═2Al(OH)+3Na2SO4+2H2O (Aluminum oxyhydroxide)| - Fe2(SO4)3+6NaOH═2FeO(OH)+3Na2SO4+2H2O (Iron oxyhydroxide)| - Fe2(SO4)3+6NaOH=Fe2O3+3Na2SO4+3H2O (hematite)| - 3Al2(SO4)3+12NaOH═2NaAl3(SO4)2(OH)6+5Na2SO4 (Alunite)| - 3Fe2(SO4)3+12NaOH═2NaFe3(SO4)2(OH)6+5Na2SO4 (Jarosite)|Nickel and Cobalt Precipitation| - NiSO4+2NaOH═Ni(OH)2+Na2SO4 | - CoSO4+2NaOH═Co(OH)2+Na2SO4 |Iron/Aluminum/Manganese Removal Stage 2| - Al2(SO4)3+6NaOH═2Al(OH)3+3Na2SO4 (Aluminum hydroxide)| - Fe2(SO4)3+6NaOH═2Fe(OH)3+3Na2SO4 (Iron hydroxide)| - Al2(SO4)3+6NaOH═2Al(OH)+3Na2SO4+2H2O (Aluminum oxyhydroxide)| - Fe2(SO4)3+6NaOH═2FeO(OH)+3Na2SO4+2H2O (Iron oxyhydroxide)| - 3Al2(SO4)3+12NaOH═2NaAl3(SO4)2(OH)6+5Na2SO4 (Alunite)| - 3Fe2(SO4)3+12NaOH═2NaFe3(SO4)2(OH)6+5Na2SO4 (Jarosite)| - MnSO4+Na2S2O8+4NaOH=MnO2+3Na2SO4+2H2O|Magnesium Hydroxide Precipitation| - MgSO4+2NaOH═Mg(OH)2+Na2SO4 |Salt Splitting (Anion Exchange Membrane)| - 2Na2SO4+4H2O=4NaOH+2H2SO4+2H2+O2 |[0168] In alternative embodiments, processes make use of NaOH, NaHCO2 or Na2CO3 precipitants, with some alternative chemistries shown below:|Neutralization| - Alkali hydroxide: H2SO4+2NaOH=Na2SO4+2H2O| - Alkali metal carbonate: H2SO4+Na2CO3=Na2SO4+H2O+CO2(g) |Iron Precipitation| - Alkali hydroxide: Fe2(SO4)3+6NaOH═2Fe(OH)3+3Na2SO4 | - or Fe2(SO4)3+6NaOH=Fe2O3+3Na2SO4+3H2O| - Alkali metal carbonate: Fe2(SO4)3+3Na2CO3+H2O ═2FeO(OH)+| - 3Na2SO4+3CO2(g) |Nickel Recovery| - Alkali hydroxide: NiSO4+2NaOH═Ni(OH)2+Na2SO4 | - Alkali metal carbonate: NiSO4+Na2CO3=NiCO3+Na2SO4 |Magnesium Recovery| - Alkali hydroxide: MgSO4+2NaOH═Mg(OH)2+Na2SO4 | - Alkali metal carbonate (with Na2CO3): MgSO4+Na2CO3=MgCO3+Na2SO4 | - Alkali metal carbonate with NaOH/CO2(g): MgSO4+2NaOH+CO2=MgCO3+Na2SO4+H2O|[0180] The present processes may be integrated with other carbon sequestration processes, such as ocean alkalinity enhancement. This present processes for the production of synthetic brucite and calcium hydroxide accordingly address environmental risks of direct ocean alkalinity enhancement with untreated mafic rocks. The present processes also create a less carbon intensive source of magnesium and calcium hydroxides to be used as feedstock in carbon capture and storage, including direct air capture technologies. The use of the brucite or calcium hydroxide products of the present processes in a direct air capture (DAC) process may be carried out so as to eliminate calcining and slacking steps that are otherwise required in these processes. The present processes provide for the use of basaltic sands in less carbon intensive industrial purposes, by producing low carbon sources of nickel and iron hydroxides as well as amorphous silicate (SiO2).|[0181] Although various embodiments of the invention are disclosed herein, many adaptations and modifications may be made within the scope of the invention in accordance with the common general knowledge of those skilled in this art. Such modifications include the substitution of known equivalents for any aspect of the invention in order to achieve the same result in substantially the same way. Terms such as “exemplary” or “exemplified” are used herein to mean “serving as an example, instance, or illustration.” Any implementation described herein as “exemplary” or “exemplified” is accordingly not to be construed as necessarily preferred or advantageous over other implementations, all such implementations being independent embodiments. Unless otherwise stated, numeric ranges are inclusive of the numbers defining the range, and numbers are necessarily approximations to the given decimal. The word “comprising” is used herein as an open-ended term, substantially equivalent to the phrase “including, but not limited to”, and the word “comprises” has a corresponding meaning. As used herein, the singular forms “a”, “an” and “the” include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to “a thing” includes more than one such thing. Citation of references herein is not an admission that such references are prior art to the present invention. Any priority document(s) and all publications, including but not limited to patents and patent applications, cited in this specification, and all documents cited in such documents and publications, are hereby incorporated herein by reference as if each individual publication were specifically and individually indicated to be incorporated by reference herein and as though fully set forth herein. The invention includes all embodiments and variations substantially as hereinbefore described and with reference to the examples and drawings. (US20240002973)|FIELD|[0001] The invention is in the field of inorganic chemistry, integrating electrochemical processes with steps of hydrometallurgical value extraction and carbon dioxide capture.|BACKGROUND|[0002] Technologies for efficient sequestration of gaseous carbon dioxide are potentially an important tool for addressing anthropogenic climate change. Various approaches have been suggested for sequestering carbon as mineral carbonates, including techniques that accelerate weathering reactions of minerals in ultramafic and mafic source rocks. These enhanced weathering (on land) or ocean alkalinity enhancement (at sea) approaches consume CO2 but are necessarily accompanied by a release of mineral dissolution products such as alkaline species and metal compounds, for example Si, Ca, Mg, Fe, Ni, and Co species. The ecological effect of these processes are uncertain (see Bach et al., CO2 Removal With Enhanced Weathering and Ocean Alkalinity Enhancement: Potential Risks and Co-benefits for Marine Pelagic Ecosystems, Frontiers in Climate, vol. 1, 2019, pg 7). There is a need for processes that integrate carbon capture with the recovery of metal values from mineral feedstocks.|SUMMARY|[0003] Processes are provided in which successive steps of hydrometallurgical value extraction are carried out on a mineral feedstock, such as an olivine, mafic, saprolite or ultramafic feedstock. In select embodiments, the products of carbon capture reactions and an electrolytic reagent-generating process are utilized as inputs to hydrometallurgical value recovery steps. The electrolytic process provides the acid leachant (HCl or H2SO4) and an alkali hydroxide (NaOH or KOH), with the alkali hydroxide then available for use either directly as a precipitant in the hydrometallurgical steps, or available for conversion to an alkali metal carbonate or bicarbonate that can in turn be used as the precipitant in the hydrometallurgical steps. In an alternative embodiment, the alkali hydroxide from the chloralkali process may be used to precipitate a calcium hydroxide product, with the calcium hydroxide product then available for use directly in carbon dioxide gas scrubbing, or for use to accept a carbonate that is provided by a CO2 scrubbing process.|[0004] Processes are accordingly provided for the coproduction from mineral feedstocks such as basaltic rocks of less carbon intensive, or carbon negative, nickel, iron, calcium and magnesium hydroxides or carbonates. Basaltic sand materials that include amorphous silicates may also be produced. These processes may involve (1) magnetic separation, (2) hydrochloric or sulfuric acid leaching, (3) selective precipitation of metal hydroxides or carbonates in successive steps, which may involve pH modulation (in select embodiments, nickel may for example be separated using a resin in leach step) (4) electrolysis of a resulting barren solution, for example a chloralkali process for treating NaCl(aq), or an electrolytic salt splitting anion exchange process for treating Na2SO4(aq), and (5) acid and alkali reagent recycling, for example in the case of a chloralkali process, hydrochloric acid production from the hydrogen and chlorine gas products of the electrolysis.|[0005] Process of the invention accordingly provide for the use of less carbon intensive nickel, iron, calcium and magnesium hydroxides or carbonates, as well as olivine and basaltic sand material, including amorphous silicates, in marketable products. These may for example include feedstocks for battery, steel, cement, tyre, glass, aggregate, or concrete industries. Products of the present processes, such as the solid siliceous residue or iron precipitate products, may for example be subject to washing and/or alkalization. The adjustment of pH by way of alkalization (alkali addition) may improve the suitability of the final product, for example to produce a siliceous residue suitable for use as a supplementary cementitious material (SCM) in cements with improved cementitious properties.|[0006] The present processes provide avenues for the coproduction of less carbon intensive nickel and iron hydroxides, and this in turn may provide avenues to decarbonate sectors associated with the transition to a low carbon economy—such as electric vehicles and batteries. The invention also facilitates low carbon steelmaking, by compensating carbon heavy pyrometallurgy with a carbon negative magnetic, hydrometallurgical and electrochemical process.|[0007] The present processes provide for the coproduction of less carbon intensive amorphous silicates, marketable as a supplementary cementitious material (SCM) for cements, or in the tyre manufacturing industry. Basaltic sand materials may be produced by the present processes, with an inert surface, for example for use as aggregate in concrete mixes. The invention accordingly facilitates the construction of less carbon intensive concrete buildings.|[0008] Processes are accordingly provided for processing a comminuted mineral feedstock, comprising:| - optionally magnetically separating material from the comminuted mineral feedstock;| - a) leaching metal values from the comminuted mineral feedstock with an acid leachant, to produce a solid siliceous residue and a loaded leach solution;| - optionally subjecting the loaded leach solution to a resin in leach process so as to selectively remove nickel and cobalt values from the loaded leach solution, to obtain a purified nickel and cobalt combined product,| - optionally, washing and/or alkalization of the solid siliceous residue, for example to form a supplementary cementitious material (SCM) for use in cements;| - b) precipitating iron and/or aluminum from the loaded leach solution with addition of: | - a first alkali metal carbonate or bicarbonate precipitant,| - to produce a carbon dioxide off gas, or, | - a first alkali hydroxide precipitant,| - to produce an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide (e.g. hematite) precipitate product;| - optionally, washing and/or alkalization of the iron and/or aluminum hydroxide precipitate product;| - optionally, adding a hematite seed material to the step of precipitating iron and/or aluminum, wherein the iron and/or aluminum hydroxide precipitate product may comprise the hematite seed material, which is then recirculated to the precipitation step;| - c) precipitating nickel and/or cobalt from the Fe/Al depleted solution or from a Ni/Co ion exchange eluant obtained from the Fe/Al depleted solution by selective extraction of Ni and/or cobalt on an ion exchange medium, wherein the precipitating is with addition of: | - a second alkali metal carbonate or alkali metal bicarbonate precipitant, or,| - a second alkali hydroxide precipitant,| - to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate or hydroxide precipitate product;| - d) before or after step (c), precipitating iron and/or aluminum and/or manganese from the Ni/Co depleted solution with addition of an oxidant and with addition of: | - a third alkali metal carbonate or bicarbonate precipitant, or,| - a third alkali hydroxide precipitant,| - to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product;| - optionally recycling a brine comprising the Fe/Al/Mn depleted solution to a comminuting step to provide the comminuted mineral feedstock;| - e) precipitating magnesium from the Fe/Al/Mn depleted solution with addition of: | - a fourth alkali hydroxide precipitant, or| - a fourth alkali metal carbonate or bicarbonate precipitant,| - to produce a Mg-depleted solution and a magnesium hydroxide or carbonate precipitate product;| - f) subjecting the Mg-depleted solution to an electrolysis process to produce the acid leachant and: | - one or more of the alkali hydroxide precipitants, or| - an alkali hydroxide product, available for conversion into one or more of the alkali metal carbonate or bicarbonate precipitants; and,| - g) optionally sequestering carbon dioxide from a CO2 containing gas, for example by reaction with the alkali hydroxide product, and/or in one or more of: the nickel and/or cobalt carbonate precipitate product; or, the magnesium hydroxide precipitate product.|[0037] Processes may further include scrubbing carbon dioxide from a CO2 containing gas, including ambient air, by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide precipitant, to produce one or more of the alkali metal carbonate or bicarbonate precipitants.|[0038] Processes are according provided for processing a comminuted mineral feedstock, comprising:| - a) leaching metal values from the comminuted mineral feedstock with an acid leachant, to produce a solid siliceous residue and a loaded leach solution;| - b) precipitating iron and/or aluminum from the loaded leach solution with addition of: | - a first alkali metal carbonate precipitant, to produce a carbon dioxide off gas, or,| - a first alkali hydroxide precipitant,| - to produce an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate (such as hematite) product;| - c) precipitating nickel and/or cobalt from the Fe/Al depleted solution or from a Ni/Co ion exchange eluant obtained from the Fe/Al depleted solution by selective extraction of nickel and/or cobalt on an ion exchange medium, wherein the precipitating is with addition of: | - a second alkali metal carbonate or bicarbonate precipitant, or,| - a second alkali hydroxide precipitant,| - to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate or hydroxide precipitate product, such as a mixed Ni/Co hydroxide product;| - d) before or after step (c), precipitating iron and/or aluminum and/or manganese from the Ni/Co depleted solution with addition of an oxidant (such as chlorine gas (Cl2(g)) or sodium hypochlorite (NaOCL)) and with addition of: | - a third alkali metal carbonate or bicarbonate precipitant, or,| - a third alkali hydroxide precipitant,| - to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product;| - e) precipitating magnesium from the Fe/Al/Mn depleted solution with addition of: | - a fourth alkali hydroxide precipitant, or| - a fourth alkali metal carbonate or bicarbonate precipitant,| - to produce a Mg-depleted solution and a magnesium hydroxide or carbonate precipitate product;| - f) subjecting the Mg-depleted solution to an electrolysis process to produce the acid leachant and: | - one or more of the alkali hydroxide precipitants, or| - an alkali hydroxide product.|[0059] Processes may further involve reacting the alkali hydroxide product of the electrolysis process directly or indirectly with a carbon source to produce one or more of the alkali metal carbonate or bicarbonate precipitants. The step of reacting the alkali hydroxide product with a carbon source may involve scrubbing carbon dioxide from a CO2 containing gas by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide product, to produce one or more of the alkali metal carbonate or bicarbonate precipitants.|[0060] In select embodiments, calcium may be precipitated from the Mg-depleted solution with a fifth alkali hydroxide precipitant, to produce a calcium hydroxide product, and generating one or more of the alkali metal carbonate or bicarbonate precipitants by treating the calcium hydroxide product with a carbon source, such as a CO2 containing gas or a metal carbonate, and the CO2 containing gas may for example be air. When the alkali hydroxide product comprises NaOH, scrubbing carbon dioxide from the CO2 containing gas may accordingly involve precipitating Na2CO3 hydrates from the scrubbing solution in a crystallisation process to produce a solid Na2CO3 crystallizer product, and one or more of the alkali metal carbonate or bicarbonate precipitants comprises the solid Na2CO3 crystallizer product.|[0061] In alternative embodiments, the alkali metal carbonate or bicarbonate precipitant may be one or more of NaHCO3, Na2CO3 or K2CO3, or a mixture thereof. The alkali hydroxide precipitant may be one or both of NaOH or KOH, or a mixture thereof. The acid leachant may for example be a mineral acid, such as HCl or H2SO4, or a mixture thereof.|[0062] The electrolysis process may involve a chloralkali process, producing the alkali hydroxide precipitant and/or the alkali hydroxide product, a Cl2(g) product and a H2(g) product. The Cl2(g) product and the H2(g) product may then be reacted to produce HCl as the acid leachant.|[0063] When the Mg-depleted solution includes Na2SO4, the electrolysis process may involve a salt splitting process that includes electrolytic generation of: the alkali hydroxide product and/or the alkali hydroxide precipitant; and, H2SO4 as the acid leachant.|[0064] Precipitating magnesium from the Fe/Al/Mn depleted solution with the alkali hydroxide precipitant, may involve addition of a CO2(g) precipitant to produce the Mg-depleted solution and the magnesium carbonate precipitate product. The CO2(g) precipitant may for example include, or be made entirely from, the carbon dioxide off gas from the step of precipitating iron and/or aluminum from the loaded leach solution.|[0065] In select embodiments, an initial step of magnetically separating material from the comminuted mineral feedstock may be implements, for example so as to enrich the feedstock in select materials.|[0066] In select embodiments, the loaded leach solution may be subjected to a resin in leach process so as to selectively remove nickel values from the loaded leach solution, to obtain a purified nickel product.|[0067] The products of the process may be further treated for example by washing and/or alkalization of the solid siliceous residue, washing and/or alkalization of the iron and/or aluminum hydroxide or oxide precipitate product.|[0068] A hematite seed material may be added to the step of precipitating iron and/or aluminum so as to seed the precipitation of a hematite product. When the iron and/or aluminum hydroxide or oxide precipitate product comprises a hematite seed material, the hematite seed material may be recirculated to the step of precipitating iron and/or aluminum so as to seed the precipitation of a hematite product.|[0069] A brine that includes some or all of the Fe/Al/Mn depleted solution may be recirculated to the comminuting step, to provide the comminuted mineral feedstock.|[0070] The mineral feedstock may for example be, or include, one or more of a nickel saprolite ore or tailing, an olivine ore or tailing, an asbestos ore or tailing, a mafic mineral, a saprolite material, an ultramafic rock, olivine, wollastonite or combinations thereof.|(US20240002973)|BRIEF DESCRIPTION OF THE DRAWINGS|[0071] FIG. 1 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process.|[0072] FIG. 2 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process.|[0073] FIG. 3 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process.|[0074] FIG. 4 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process.|[0075] FIG. 5 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process, showing the use of Na2CO3 to precipitate Mg.|[0076] FIG. 6 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide and a chloralkali electrochemical process, showing the use of NaOH in combination with CO2(g) to precipitate Mg.|[0077] FIG. 7 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by an electrolytic salt splitting anion exchange process.|[0078] FIG. 8 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide (DAC) and an electrolytic salt splitting anion exchange process.|[0079] FIG. 9 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide (DAC) and an electrolytic salt splitting anion exchange process.|[0080] FIG. 10 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, with reactants for the hydrometallurgical process provided by capture of carbon dioxide (DAC) and an electrolytic salt splitting anion exchange process.|[0081] FIG. 11 is a schematic illustration of an integrated process for hydrometallurgical value extraction from a mineral feedstock, which includes an initial step of magnetic beneficiation to adjust the metal content of the treated material.|(US20240002973)|DETAILED DESCRIPTION|[0082] Processes are provided in which successive steps of hydrometallurgical value extraction are carried out using the products of carbon capture and an electrolytic reactant regeneration process, such as a chloralkali process or an electrolytic salt splitting anion exchange process. The electrolytic reactant regeneration process provides an acid leachant and an alkali hydroxide, with the alkali hydroxide (e.g. NaOH) then available for use either directly as a precipitant in the hydrometallurgical steps, or available for conversion to an alkali metal carbonate (e.g. Na2CO3) or bicarbonate (e.g. NaHCO3) that can in turn be used as the precipitant in the hydrometallurgical steps.|[0083] In an alternative embodiment, the alkali hydroxide from the chloralkali process may be used to precipitate a calcium hydroxide product, with the calcium hydroxide product then available for use directly in carbon dioxide gas scrubbing, or for use to accept a carbonate that is provided by a CO2 scrubbing process.|[0084] In some embodiments, a crystalliser step may be introduced to precipitate Na2CO3 or Na2CO3 hydrates from a CO2 enriched solution that is being treated with the alkali hydroxide (NaOH) product of the chloralkali process. In such processes, a crystalliser may be used to reduce water content in the hydrates by modulating temperature, pressure and NaOH concentration. The solid Na2CO3 product may then be used as a carbonate precipitant.|[0085] By using a carbonate precipitant to precipitate iron and aluminum from the leach solution, at a suitably low pH, the carbonate will decompose to release a concentrated stream of CO2, and the concentrated CO2 stream may in turn be sequestered or fixed.|[0086] FIG. 1 illustrates a process in which metal values are leached from a comminuted (“crushing and grinding”) mineral feedstock with an acid leachant (“HCl leaching”), to produce a solid siliceous residue (“Amorphous Silica Residue for Cement Manufacture”) and a loaded leach solution. As illustrated, the residue may be washed. Crushing and grinding in a recycled brine solution containing a variety of chloride or sulfate salts, such as magnesium and sodium salts, may be carried out so as to avoid or minimize the need for the addition of non-brine water. HCl acid leaching may be carried out at relatively high acid concentrations, such as 30-36% HCl by weight in water—a typical product from an HCl production facility attached to a chlor-alkali plant.|[0087] As illustrated in FIG. 11, in an embodiment of the invention, the ferromagnetic content of the crushed ore may be modulated using a magnetic separator, for example so as to increase or decrease the iron and nickel hydroxide products of the process. For example, with an (ultra)mafic sand input comprising olivine or wollastonite, the ratio of MgSiO4 and CaSiO4 content to nickel and iron may be optimised via magnetic separation. In a further alternative, a resin in leach process may be used to selectively remove nickel content in the acidic leach prior to selective precipitation steps, to obtain a purified nickel product.|[0088] Conditions for leaching may include a leaching temperature of from 80° C. to boiling point, to 115° C. or higher. Acid addition during HCl leaching may for example range from 500 to 1000 kg HCl per dry tonne of solid feed, varying with the chemical composition of the feed. Leaching times may for example be for effective residence times of from 1 hour to 8 hours. Leaching may for example be carried out in a single stage or two or more countercurrent stages. In a single stage process, the acid and ore are added together and allowed to react at a leaching temperature to completion. In a multistage leach, fresh ore is contacted with partly reacted solution so as to maximize the use of the acid (low terminal acidity) and in the second or subsequent stage, the partly leached ore (from the first stage) is contacted with high acid to maximize extraction of Mg/Ni/Co/Fe, etc. The multistage process may involve additional solid/liquid separation steps to ensure countercurrent movement of solids and liquids.|[0089] The raw materials for the present processes may contain a variety of silicate minerals including magnesium, iron, nickel and cobalt and minor impurity elements. The chemistry of acid leaching, with HCl, may therefore be represented the following reactions:|Mg2SiO4+4HCl=2MgCl2+SiO2+2H2O|Ni2SiO4+4HCl=2NiCl2+SiO2+2H2O|Fe2SiO4+4HCl=2FeCl2+SiO2+2H2O|[0090] Other minerals present in source materials such as iron oxides or aluminum oxides may also react with HCl to form additional salts in solution:|FeO(OH)+3HCl=FeCl3+2H2O|AlO(OH)+3HCl=AlCl3+2H2O|[0091] Natural mineral source materials are of course not pure compounds, so that the source minerals my contain a variety of elements (eg. Mg, Ni, Co, Fe in one silicate mineral) and may be hydrated or weathered. Geological descriptions of suitable feed materials include: nickel saprolite ores, olivine ores, and asbestos ores and tailings.|[0092] The product of HCl leaching is a weakly acidic solution containing various chloride salts. A silica rich residue is recovered as a solid product. This residue may for example be washed to remove salts and excess acid with fresh water, and/or alkalized (alkali conditioning) with a base to adjust pH, and then directed to cement manufacture where the silica may be used as a replacement for other materials (thus lowering the carbon intensity of cement manufacture) and as a strengthener to improve the yield strength of concrete, with the silica acting as a supplementary cementitious material (SCM) in a high performance concrete.|[0093] Iron and/or aluminum are precipitated (“Iron and Aluminum Precipitation”) from the loaded leach solution with an alkali hydroxide (NaOH) or alkali metal carbonate or bicarbonate precipitant (Na2CO3 as illustrated in FIG. 1). When Na2CO3 is used as a precipitant, this produces a carbon dioxide off gas (“CO2 Off Gas”), an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate product (“Fe/Al Hydroxide Precipitate” as illustrated, comprising magnetite in select embodiments). As illustrated, the residue is washed to provide the precipitate. When an alkali hydroxide (e.g. KOH or NaOH) is used as the precipitant, the iron and aluminum content in the solution is generally precipitated as a mix of oxide and hydroxide solids by raising the pH with an alkali hydroxide (KOH or NaOH) solution. The NaOH solution may for example be added as a 50% solution, and may be diluted with recycled brine solution for process convenience and enhanced pH control (it may be hard to control pH when adding a very strong base). The added NaOH neutralizes excess acid and precipitates Fe/Al and other trivalent cations if present:|HCl+NaOH=NaCl+H2O|FeCl3+3NaOH═FeO(OH)+3NaCl+H2O|2FeCl3+6NaOH═Fe2O3(hematite)+6NaCl+3H2O|AlCl3+3NaOH═AlO(OH)+3NaCl+H2O|2AlCl3+6NaOH=Al2O3+6NaCl+3H2O|CrCl3+3NaOH═CrO(OH)+3NaCl+H2O|2CrCl3+6NaOH=Cr2O3+6NaCl+3H2O|[0094] The pH adjustment may for example be conducted with stoichiometric amounts of alkali hydroxide. Over-addition of NaOH may result in precipitation of Ni/Co (undesirable) so control of base addition must be maintained. The Fe/Al precipitation temperature may for example be 75° C. to boiling point. Seed (precipitate) may be recycled, for example in the form of hematite, to ensure growth of suitably sized particles, and materials, for enhanced solid/liquid separation. An initial mineral seed, such as hematite, may be used to initiate the process of precipitating a select material, such as hematite. Fe/Al precipitation time may for example be 1 to 8 hours. NaOH may for example be added progressively through precipitation tanks (continuous) so as to enhance precipitation of coarser/separable precipitates. The Fe/Al precipitation product may be separated by S/L separation and washed.|[0095] The Fe/Al precipitation residue may for example be treated to form commercial products, such as hematite. For example, drying and partial reduction may be used to form magnetite and a mixed Al/Cr oxide. The magnetite can be separated using magnetic separation and the Al/Cr oxide can be sold as a product for the refractory market.|[0096] Nickel and cobalt may be selectively recovered in a variety of ways. In an HCl based leaching process, Ni and Co will be present in solution as NiCl2 and CoCl2 salts, and these salts can be recovered by ion exchange, for example using a Dow M4195 resin to extract Ni and Co in a Na-form resin. The resin can then be stripped with HCl solution to form a strong, purified solution of Ni/Co chloride salts. The resin may then be treated with NaOH solution after acid stripping to return to the resin “loading” step.|[0097] In select embodiments, the recovery of Ni/Co is by way of a mixed hydroxide precipitate (MHP). This can be done directly from the solution coming from the iron precipitation step, or can be effected starting with the ion exchange eluant containing nickel and cobalt chloride. In these processes, a solution of sodium hydroxide is added to from the precipitates:|NiCl2+2NaOH═Ni(OH)2+2NaCl|CoCl2+2NaOH═Co(OH)2+2NaCl|[0098] Other metals may also precipitate with the Ni/Co in minor amounts. For example Mn, Fe (remaining iron in solution).|[0099] The selectivity of Ni/Co MHP precipitation can be enhanced by using two stage MHP precipitation, in which a second stage precipitate is recovered and recycled to the first stage or to the discharge from the main leaching step (where acid is present to redissolve the Ni/Co and other metals from the second stage leach).|[0100] The mixed hydroxide precipitate may be recovered by S/L separation and washing. A pressure filter may be used with a “squeeze” cycle to minimize the entrained moisture in the washed Ni/Co MHP cake prior to shipping.|[0101] The Ni/Co MHP precipitation may be carried out between 25-90° C. with a terminal pH in the range of 5-8. The addition of base can also be controlled by stoichiometry rather than, or in addition to, pH. The Ni/Co MHP precipitation time may for example be 1-8 hours. Seed recycling may be used to maximize particle size and minimize contamination. The Ni/Co MHP process (as in all steps) may be conducted continuously.|[0102] As illustrated in FIG. 1, in an alternative embodiment nickel and/or cobalt may be precipitated from the Fe/Al depleted solution with a second alkali metal carbonate or bicarbonate precipitant (Na2CO3 as illustrated), to produce a Ni/Co depleted solution and a nickel and/or cobalt carbonate precipitate product (“Ni/Co Carbonate (to battery manufacture)”).|[0103] Most of the iron and aluminum are removed from solution in the first iron removal step. Manganese is generally not removed from solution in either the initial iron control or the Ni/Co MHP precipitation steps. Accordingly, a second stage of iron precipitation may be implemented with increased pH so as to maximize the removal of iron with an oxidant added to oxidize Mn and Fe to facilitate more complete removal and purification of all species. Suitable oxidants include gaseous chlorine or sodium hypochlorite (NaOCl). Example reactions include:|2FeCl2+NaOCl+4NaOH═2FeO(OH)+5NaCl+H2O|MnCl2+NaOCl+2NaOH=MnO2+3NaCl+H2O|AlCl3+3NaOH═AlO(OH)+3NaCl+H2O|[0104] Conditions for iron and/or aluminum and/or manganese scrubbing may be designed to maximize precipitation of the impurity elements while minimizing formation of magnesium hydroxide. The oxidant (eg. NaOCl) may be added so as to achieve a suitably high oxidation/reduction potential (ORP) to maximize the oxidative removal of Fe/Mn. Scrubbing temperature may for example be 25° C. to the boiling point. As in other precipitation steps, seed recycle can be used to improve performance. Scrubbing time may for example be 1 to 8 hours.|[0105] Alternatively, as illustrated in FIG. 1, iron and/or aluminum and/or manganese may be scrubbed from the Ni/Co depleted solution with a third alkali metal carbonate or bicarbonate precipitant (also Na2CO3 as illustrated) and an oxidant, such as the illustrated sodium hypochlorite, to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product (“Fe/Al/Mn Hydroxide Precipitate”). As illustrated, brine comprising the Fe/Al/Mn depleted solution may be recycled to the comminuting step to provide the comminuted mineral feedstock.|[0106] Magnesium remaining in solution may be precipitated from the Fe/Al/Mn depleted solution with an alkali hydroxide precipitant (NaOH as illustrated), to produce a Mg-depleted solution and a magnesium hydroxide precipitate product (“Mg Hydroxide Precipitate”):|MgCl2+2NaOH═Mg(OH)2+2NaCl|[0107] This may for example be carried out by adding NaOH to MgCl2 solution, or by reversing the order of addition. In either case, the process may be carried out so as to provide a near complete removal of Mg as Mg(OH)2 from solution. This generally requires a near stoichiometric addition of NaOH.|[0108] The Mg-depleted solution may then be subjected to further purification, for example in an ion exchange resin separation step, or sent directly to an electrolysis to produce the alkali hydroxide precipitant and the acid leachant (in FIG. 1, “Chlor-Alkali Plant to make HCl and NaOH for Recycle”, in FIG. 7 “Salt Splitting Plant to make H2SO4 and NaOH for Recycle”). Standard chloralkali brine pretreatments may be carried out on the Mg-depleted solution to provide a higher purity Mg-depleted brine, for example essentially free of undesirable solids and ions, for example involving brine saturation/evaporation and softening, for example by primary and polish filtration steps and high-performance ion exchange softening. In an HCl based extraction process, the final Mg-depleted solution is NaCl(aq) with some minor contaminants in solution. This NaCl(aq) solution is directed to a chlor-alkali plant for manufacture of NaOH, Cl2 and H2, involving conventional steps, with the Cl2 and H2 available to be burned and water-scrubbed to form a strong HCl solution for recycle to leaching. Excess heat from Cl2 and H2 combustion may for example be recovered as steam and used to evaporate excess water from solution.|[0109] As illustrated in FIG. 1, carbon dioxide may be scrubbed from a CO2 containing gas (“Air” as illustrated) by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide precipitant (NaOH as illustrated), to produce one or more of the alkali metal carbonate or bicarbonate precipitants (Na2CO3 as illustrated).|[0110] In the foregoing process, the step of scrubbing carbon dioxide from the CO2 containing gas may include a crystallisation step to precipitate Na2CO3 hydrates from the scrubbing solution, the alkali hydroxide precipitant being NaOH. The solid Na2CO3 crystallizer product may then be directed to provide one or more of the alkali metal carbonate or bicarbonate precipitants.|[0111] FIG. 2 illustrates a process analogous to the process illustrated in FIG. 1, with potassium compounds in place of the sodium compounds of FIG. 1.|[0112] FIG. 3 and FIG. 4 illustrate alternative embodiments which involve precipitating calcium from the Mg-depleted solution with a fourth alkali metal hydroxide precipitant (NaOH as illustrated), to produce a Ca-depleted solution and a calcium hydroxide product. The calcium hydroxide product is then available for carbon sequestration reactions, for example by generating the metal carbonate precipitant for the iron and/or aluminum precipitation step by treating the calcium hydroxide product with a carbon source, such as air (FIG. 3) or a metal carbonate that is in turn derived from KOH-mediated carbon capture (FIG. 4). In these processes, the Ca-depleted solution is subjected to electrolysis to produce one or more of the first, second, third or fourth alkali metal hydroxide precipitants and the acid leachant.|[0113] The alkali hydroxide precipitant may accordingly be NaOH (FIGS. 1, 3 and 4) or KOH (FIG. 2). The process acid leachant as illustrated is HCl. These products may be produced in a chloralkali process.|[0114] FIG. 5 and FIG. 6 illustrate alternative embodiments, in which alternative pathways are used to form MgCO3 rather than Mg(OH)2 in the magnesium precipitation step. These embodiments reflect adaptations related to the use of Mg(OH)2 from the present processes for: (1) direct air capture (DAC) of CO2 to form MgCO3; or, (2) ocean alkalinity enhancement (OAE) to form Mg(HCO3)2 by direct addition of Mg(OH)2 to the ocean environment. The use of Mg(OH)2 to form MgCO3 by contact with air containing CO2 can in some circumstances suffer from unfavourable kinetics. The embodiments illustrated in FIG. 5 and FIG. 6 accordingly provide alternative routes to forming MgCO3 in approaches that may be adapted to optimize carbon sequestration.|[0115] FIG. 5 illustrates a process in which MgCO3 is formed by direct neutralization of the Fe/Al/Mn depleted solution, so that Na2CO3, for example produced in and recovered from a direct air capture (DAC) process, reacts with MgCl2 (aq) in the Fe/Al/Mn depleted solution to form MgCO3(s):|MgCl2+Na2CO3=MgCO3+2NaCl|[0116] In select embodiments, essentially the full amount of NaOH produced by the chloralkali process is directed to the DAC system to produce Na2CO3 from CO2 captured directly from the atmosphere. In such a process, sufficient Na2CO3 is produced to provide the alkali metal precipitant for all aspects of the process, including recovery of MgCO3. In this way, sorbent regeneration for DAC, i.e. NaOH, is combined with long term mineralisation of the CO2. MgCO3 mineralisation thereby creates carbon negative products in the form of carbonates, that may for example be used as filler or construction aggregate.|[0117] FIG. 6 illustrates an alternative process involving the formation of MgCO3 by direct addition of CO2 gas, with addition of NaOH, to the Fe/Al/Mn depleted solution, to react with MgCl2 (aq) in solution to form MgCO3(s):|MgCl2+2NaOH+CO2(g)=MgCO3+2NaCl+H2O|[0118] As illustrated in FIG. 6, a portion of NaOH from the chloralkali process may be directed to the Mg precipitation stage, together with CO2(g) (for example recovered as a CO2 off gas from iron and aluminum precipitation with Na2CO3), forming MgCO3 in-situ. Alternatively, CO2(g) for Mg carbonate precipitation may come from sources external to the present process.|[0119] Reactions in various stages of the present process may be represented as follows:|Neutralization| - Alkali hydroxide: 2HCl+2NaOH=2NaCl+2H2O| - Alkali metal carbonate: 2HCl+Na2CO3=2NaCl+H2O+CO2(g) |Iron Precipitation| - Alkali hydroxide: 2FeCl3+6NaOH═2FeO(OH)+2H2O+6NaCl | - 2FeCl3+6NaOH═Fe2O3 (hematite)+6NaCl+3H2O| - Alkali metal carbonate: 2FeCl3+3Na2CO3+H2O ═2FeO(OH)+6NaCl+3CO2(g) |Nickel Recovery| - Alkali hydroxide: NiCl2+2NaOH═Ni(OH)2+2NaCl| - Alkali metal carbonate: NiCl2+Na2CO3=NiCO3+2NaCl|Magnesium Recovery| - Alkali hydroxide: MgCl2+2NaOH═Mg(OH)2+2NaCl| - Alkali metal carbonate: MgCl2+Na2CO3=MgCO3+2NaCl| - Direct CO2: MgCl2+2NaOH+CO2(g)=MgCO3+2NaCl+H2O|[0130] In alternative embodiments, NaHCO3 may take the place of Na2CO3 in reactions in various stages of the present process.|[0131] FIGS. 7-10 illustrate processes in which metal values are leached from a comminuted (“crushing and grinding”) mineral feedstock with a sulfuric acid leachant (“H2SO4 leaching”), to produce a solid siliceous residue (“Amorphous Silica Residue for Cement Manufacture”) and a loaded leach solution. As illustrated, the residue may be washed.|[0132] Iron and/or aluminum are precipitated (“Iron and Aluminum Precipitation”) from the loaded leach solution with either an alkali hydroxide precipitant (FIG. 7) or an alkali metal carbonate or bicarbonate precipitant (Na2CO3 FIGS. 8-10). Use of the alkali metal carbonate or bicarbonate precipitant produces a carbon dioxide off gas (“CO2 Off Gas”), an Fe/Al depleted solution and an iron and/or aluminum hydroxide or oxide precipitate product (“Fe/Al Hydroxide Precipitate”, which may be an oxide, such as hematite). The concentrated CO2 Off Gas may be sequestered using a variety of approaches. As illustrated, the residue may be washed to provide the precipitate, and the precipitate may be used in magnetite manufacture.|[0133] Nickel and/or cobalt are precipitated from the Fe/Al depleted solution with the alkali hydroxide precipitant (e.g. NaOH, FIG. 7) or the alkali metal carbonate or bicarbonate precipitant (e.g. Na2CO3, FIGS. 8-10), to produce a Ni/Co depleted solution and a nickel and/or cobalt hydroxide (FIG. 1, “MHP”) or carbonate precipitate product (FIGS. 8-10, “Ni/Co Carbonate (to battery manufacture)”).|[0134] Iron and/or aluminum and/or manganese may be scrubbed from the Ni/Co depleted solution with the alkali hydroxide precipitant (FIG. 7) or with the alkali metal carbonate or bicarbonate precipitant (FIGS. 8-10, Na2CO3) and an oxidant, such as the illustrated sodium persulfate (Na2S2O8), to produce an Fe/Al/Mn depleted solution and an iron and/or aluminum and/or manganese hydroxide precipitate product (“Fe/Al/Mn Hydroxide Precipitate”).|[0135] As illustrated, brine comprising the Fe/Al/Mn depleted solution may be recycled to the comminuting step to provide the comminuted mineral feedstock.|[0136] Magnesium may be precipitated from the Fe/Al/Mn depleted solution with the alkali hydroxide precipitant (NaOH as illustrated in FIGS. 7 and 8), or with the alkali metal carbonate or bicarbonate precipitant (FIG. 9) or with a combined feed of the alkali hydroxide precipitant and CO2 (in a carbon dioxide capture step,|[0137] FIG. 10) to produce a Mg-depleted solution and a magnesium hydroxide (FIGS. 7 and 8) or carbonate (FIGS. 9 and 10) precipitate product, The Mg-depleted solution may then be subjected to an electrolysis to produce the alkali hydroxide precipitant and the acid leachant (“Salt Splitting Plant to make H2SO4 and NaOH for Recycle”).|[0138] Carbon dioxide may be scrubbed from a CO2 containing gas (“Air” as illustrated) by treating the CO2 containing gas with a scrubbing solution comprising the alkali hydroxide precipitant (NaOH as illustrated), to produce one or more of the first, second, third and fourth alkali metal carbonate or bicarbonate precipitants (Na2CO3 as illustrated), for use respectively in i) iron and aluminum precipitation, ii) Ni/Co precipitation, iii) iron and aluminum precipitation with manganese removal, and iv) Mg precipitation.|[0139] In the foregoing process, the step of scrubbing carbon dioxide from the CO2 containing gas may include a crystallisation step to precipitate Na2CO3 hydrates from the scrubbing solution, the alkali hydroxide precipitant being NaOH. The solid Na2CO3 crystalizer product may then be directed to provide one or more of the alkali metal carbonate or bicarbonate precipitants.|[0140] The process acid leachant as illustrated is H2SO4. As such, processes are provided that use of a sulfate based system for treatment of magnesium silicates. In select embodiments, (FIG. 7) H2SO4/NaOH/Na2SO4 salt splitting is used to produce amorphous silica for cementing, iron residue, mixed nickel and cobalt hydroxide and magnesium hydroxide—which is then available for carbon sequestration. In alternative embodiments, various direct air carbon capture (DAC) steps are integrated into the sulfate system (FIGS. 8-10). In particular, FIG. 8 illustrates a process wherein a portion of the alkali hydroxide precipitant NaOH is used to remove CO2 from air. The resulting sodium carbonate is then used in the iron removal and the nickel/cobalt precipitation stages. FIG. 9 illustrates a process in which there is complete use of NaOH for DAC to form Na2CO3. The addition of Na2CO3 to the Mg precipitation stage results in MgCO3 precipitation directly for carbon sequestration. FIG. 10 illustrates an alternative embodiment in which the alkali hydroxide precipitant NaOH is combined with CO2 added directly to the Mg precipitation stage, to form MgCO3.|[0141] Steps in the sulfate process may be characterized by reactions therein, as follows:|Acid leaching (simplified);| - Mg2SiO4+2H2SO4=2MgSO4+SiO2+2H2O| - Ni2SiO4+2H2SO4=2NiSO4+SiO2+2H2O| - Co2SiO4+2H2SO4=2CoSO4+SiO2+2H2O| - Fe2SiO4+2H2SO4=2FeSO4+SiO2+2H2O| - MnO2+2FeSO4+2H2SO4=MnSO4+Fe2(SO4)3+2H2O| - 2FeO(OH)+3H2SO4═Fe2(SO4)3+4H2O| - 2Al(OH)+3H2SO4═Al2(SO4)3+4H2O|Iron/aluminum removal (with product);| - H2SO4+2NaOH=Na2SO4+2H2O| - Al2(SO4)3+6NaOH═2Al(OH)3+3Na2SO4 (Aluminum hydroxide)| - Fe2(SO4)3+6NaOH═2Fe(OH)3+3Na2SO4 (Iron hydroxide)| - Al2(SO4)3+6NaOH═2Al(OH)+3Na2SO4+2H2O (Aluminum oxyhydroxide)| - Fe2(SO4)3+6NaOH═2FeO(OH)+3Na2SO4+2H2O (Iron oxyhydroxide)| - Fe2(SO4)3+6NaOH=Fe2O3+3Na2SO4+3H2O (hematite)| - 3Al2(SO4)3+12NaOH═2NaAl3(SO4)2(OH)6+5Na2SO4 (Alunite)| - 3Fe2(SO4)3+12NaOH═2NaFe3(SO4)2(OH)6+5Na2SO4 (Jarosite)|Nickel and Cobalt Precipitation| - NiSO4+2NaOH═Ni(OH)2+Na2SO4 | - CoSO4+2NaOH═Co(OH)2+Na2SO4 |Iron/Aluminum/Manganese Removal Stage 2| - Al2(SO4)3+6NaOH═2Al(OH)3+3Na2SO4 (Aluminum hydroxide)| - Fe2(SO4)3+6NaOH═2Fe(OH)3+3Na2SO4 (Iron hydroxide)| - Al2(SO4)3+6NaOH═2Al(OH)+3Na2SO4+2H2O (Aluminum oxyhydroxide)| - Fe2(SO4)3+6NaOH═2FeO(OH)+3Na2SO4+2H2O (Iron oxyhydroxide)| - 3Al2(SO4)3+12NaOH═2NaAl3(SO4)2(OH)6+5Na2SO4 (Alunite)| - 3Fe2(SO4)3+12NaOH═2NaFe3(SO4)2(OH)6+5Na2SO4 (Jarosite)| - MnSO4+Na2S2O8+4NaOH=MnO2+3Na2SO4+2H2O|Magnesium Hydroxide Precipitation| - MgSO4+2NaOH═Mg(OH)2+Na2SO4 |Salt Splitting (Anion Exchange Membrane)| - 2Na2SO4+4H2O=4NaOH+2H2SO4+2H2+O2 |[0168] In alternative embodiments, processes make use of NaOH, NaHCO2 or Na2CO3 precipitants, with some alternative chemistries shown below:|Neutralization| - Alkali hydroxide: H2SO4+2NaOH=Na2SO4+2H2O| - Alkali metal carbonate: H2SO4+Na2CO3=Na2SO4+H2O+CO2(g) |Iron Precipitation| - Alkali hydroxide: Fe2(SO4)3+6NaOH═2Fe(OH)3+3Na2SO4 | - or Fe2(SO4)3+6NaOH=Fe2O3+3Na2SO4+3H2O| - Alkali metal carbonate: Fe2(SO4)3+3Na2CO3+H2O ═2FeO(OH)+| - 3Na2SO4+3CO2(g) |Nickel Recovery| - Alkali hydroxide: NiSO4+2NaOH═Ni(OH)2+Na2SO4 | - Alkali metal carbonate: NiSO4+Na2CO3=NiCO3+Na2SO4 |Magnesium Recovery| - Alkali hydroxide: MgSO4+2NaOH═Mg(OH)2+Na2SO4 | - Alkali metal carbonate (with Na2CO3): MgSO4+Na2CO3=MgCO3+Na2SO4 | - Alkali metal carbonate with NaOH/CO2(g): MgSO4+2NaOH+CO2=MgCO3+Na2SO4+H2O|[0180] The present processes may be integrated with other carbon sequestration processes, such as ocean alkalinity enhancement. This present processes for the production of synthetic brucite and calcium hydroxide accordingly address environmental risks of direct ocean alkalinity enhancement with untreated mafic rocks. The present processes also create a less carbon intensive source of magnesium and calcium hydroxides to be used as feedstock in carbon capture and storage, including direct air capture technologies. The use of the brucite or calcium hydroxide products of the present processes in a direct air capture (DAC) process may be carried out so as to eliminate calcining and slacking steps that are otherwise required in these processes. The present processes provide for the use of basaltic sands in less carbon intensive industrial purposes, by producing low carbon sources of nickel and iron hydroxides as well as amorphous silicate (SiO2).|[0181] Although various embodiments of the invention are disclosed herein, many adaptations and modifications may be made within the scope of the invention in accordance with the common general knowledge of those skilled in this art. Such modifications include the substitution of known equivalents for any aspect of the invention in order to achieve the same result in substantially the same way. Terms such as “exemplary” or “exemplified” are used herein to mean “serving as an example, instance, or illustration.” Any implementation described herein as “exemplary” or “exemplified” is accordingly not to be construed as necessarily preferred or advantageous over other implementations, all such implementations being independent embodiments. Unless otherwise stated, numeric ranges are inclusive of the numbers defining the range, and numbers are necessarily approximations to the given decimal. The word “comprising” is used herein as an open-ended term, substantially equivalent to the phrase “including, but not limited to”, and the word “comprises” has a corresponding meaning. As used herein, the singular forms “a”, “an” and “the” include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to “a thing” includes more than one such thing. Citation of references herein is not an admission that such references are prior art to the present invention. Any priority document(s) and all publications, including but not limited to patents and patent applications, cited in this specification, and all documents cited in such documents and publications, are hereby incorporated herein by reference as if each individual publication were specifically and individually indicated to be incorporated by reference herein and as though fully set forth herein. The invention includes all embodiments and variations substantially as hereinbefore described and with reference to the examples and drawings. Family Number|(100294161)|100294161|Abstract|(VN--98973 A)|The invention refers to processes for processing small crushed raw mineral materials. The processes in question where successive steps of extracting metallic composition by hydrometallurgy can be done using the products of carbon capture processes and producing electrophilic reagents. The electrolysis process offers acid and alkali hydroxide maceration, with alkali hydroxide then readily available for use directly as a precipitate in hydrometallurgical steps, or available for conversion by capturing carbon into carbonate of alkali metals that can be used as a precipitate in selective hydrometallurgical steps. Fig.1|CPC codes|(WO2022113025 A3)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(CA3198500 A1)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(AU2021389080 A9)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(IL-303119 A)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(CO2023007635 A2)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(KR20230110773 A)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(DO202300105 A)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(CN116802326 A)|C01F - 005/22 |C01F - 005/24 |C01F - 011/02 |C01F - 011/18/1 |C01G - 049/00/45 |C01G - 049/00/72 |C01G - 053/00 |(EP4251775 A4)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(PE202301629 A1)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(JP2023553314 A5)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(CL202301495 A1)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(US20240002973 A1)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(CR202300285 A)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(EC2346201 A)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(MX2023006141 A)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|(ZA202305467 B)|C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|IPC codes|(EP4251775 A4)|C01D-001/40|C01F-011/02|C01G-049/00|(JP2023553314 A5)|C01F-005/24|C01G-049/00|C01G-053/00|Title|(WO2022113025 A3)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(WO2022113025 A2)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(BR112023010037 A2)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(BR112023010037 A0)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(CA3198500 A1)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(AU2021389080 A1)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(AU2021389080 A9)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(IL-303119 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(CO2023007635 A2)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(KR20230110773 A)|Integration of carbon sequestration with selective wet smelting recovery of metal feces|(DO202300105 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(EP4251775 A2)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(EP4251775 A4)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(TH20230002998 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(PE202301629 A1)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(JP2023553314 A5)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(CL202301495 A1)|Integration of carbon sequestration with selective hydrometallurgical recovery of metallic values|(US20240002973 A1)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(CR202300285 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(EC2346201 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(MX2023006141 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values.|(ID202304650 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(IN202317042083 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(VN--98973 A)|Processing process of crushed raw mineral materials|(SG11202303717V A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(ZA202305467 B)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(HK40100255 A)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values|(AE20236001220 A1)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values| Materials, metallurgy|Surface technology, coating C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|C22B-003/08|C22B-003/10|C22B-003/22|C22B-003/42|C22B-003/44|C22B-021/00/15|C22B-023/0423|C22B-023/043|C22B-023/0453|C22B-023/0461|C22B-023/0484|C22B-026/22|C22B-047/00|C25B-001/04|C25B-001/22|C25B-001/34|Y02P-010/146|Y02P-010/20 C01F-005/22|C01F-005/24|C01F-011/02|C01F-011/18/1|C01G-049/00/45|C01G-049/00/72|C01G-053/00|C22B-003/08|C22B-003/10|C22B-003/22|C22B-003/42|C22B-003/44|C22B-021/00/15|C22B-023/0423|C22B-023/043|C22B-023/0453|C22B-023/0461|C22B-023/0484|C22B-026/22|C22B-047/00|C25B-001/04|C25B-001/22|C25B-001/34|Y02P-010/146|Y02P-010/20 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87322590 WHO=Examiner SELF=N CAT=A|WO202011766 87322590 WHO=Examiner SELF=N CAT=A|US20200157696 81075912 WHO=Examiner SELF=N CAT=A|US20200157696 81075912 WHO=Examiner SELF=N CAT=A|US20170240432 77019172 WHO=Examiner SELF=N CAT=A|US20170240432 77019172 WHO=Examiner SELF=N CAT=A|US20160265082 65038644 WHO=Examiner SELF=N CAT=A|US20160265082 65038644 WHO=Examiner SELF=N CAT=A|WO2011114000 37907 WHO=Examiner SELF=N CAT=A|US20120186398 2473494 WHO=Examiner SELF=N CAT=A|US20120186398 2473494 WHO=Examiner SELF=N CAT=A|CN112226630 92326676 WHO=Examiner SELF=N|JP2017520687 72005228 WHO=Examiner SELF=N|WO2015192762 107643212 WHO=Examiner SELF=N|US20150202568 70319445 WHO=Examiner SELF=N|WO201558239 69206214 WHO=Examiner SELF=N|WO2013188922 61257960 WHO=Examiner SELF=N|US20110091366 6949869 WHO=Examiner SELF=N|JP2011025241 5052696 WHO=Examiner SELF=N|US20080105088 73734924 WHO=Examiner SELF=N|JP2009535198 1046021 WHO=Examiner SELF=N|JP2009517548 61891270 WHO=Examiner SELF=N|WO200739665 6507153 WHO=Examiner SELF=N ||US20170159190; US20110091366; US20160265082; WO202011766; US20200157696; US20170240432; US20120186398|||||||US20170159190; US20110091366; US20160265082; WO202011766; US20200157696; US20170240432; US20120186398; WO2011114000|JP2011025241; JP2017520687; JP2009517548; JP2009535198; US20110091366; CN112226630||US20150202568; US20080105088; WO200739665; WO201558239; WO2015192762; WO2013188922|||||US20090169452; US20170159190||||||| |(US20240002973)|Search Report references [Examiner]|-Roque´-Rosell, J., et al. “The accumulation of Ni in serpentines and gernierites from the Falcondo Ni-laterite deposit (Dominican Republic) elucidated by means of μXAS. Geochimica et Cosmochimica Acta 198 (2017) 48-69. (Year: 2017)|-Shaikh, A. A., et al. In situ observation of the conversion of sodium carbonate to sodium carbonate monohydrate in aqueous suspension. Ind. Eng. Chem. Res. 2005, 44, 9921-9930. (Year: 2005)|-English translation of WO-2015192762-A1. (Year: 2015)|||||||||||||||||||||||| GRANTED (EP4251775)|PENDING|(US20240002973)|PENDING|(WO2022/113025)|LAPSED|(JP2023553314)|PENDING|(CN116802326)|PENDING|(ZA202305467)|GRANTED|(AEP6001220/2023)|PENDING|(IN202317042083)|PENDING|(AU2021389080)|PENDING|(HK40100255)|PENDING|(VN98973)|PENDING|(CR20230285)|PENDING|(CL2023001495)|PENDING|(ECSP23046201)|PENDING|(PE20231629)|PENDING|(TH2301002998)|PENDING|(DOP2023000105)|PENDING|(KR10-2023-0110773)|PENDING|(CO2023007635)|PENDING|(IL303119)|PENDING|(SG11202303717V)|PENDING|(BR112023010037)|PENDING|(ID2023/04650)|PENDING|(MX2023006141)|PENDING|(CA3198500)|PENDING ALIVE 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ZA|(JP2023553314)|JP|(CN116802326)|CN|(ZA202305467)|ZA|(AEP6001220/2023)|AE|(IN202317042083)|IN|(AU2021389080)|AU|(HK40100255)|HK|(VN98973)|VN|(CR20230285)|CR|(CL2023001495)|CL|(ECSP23046201)|EC|(PE20231629)|PE|(TH2301002998)|TH|(DOP2023000105)|DO|(KR10-2023-0110773)|KR|(CO2023007635)|CO|(IL303119)|IL|(SG11202303717V)|SG|(BR112023010037)|BR|(ID2023/04650)|ID|(MX2023006141)|MX|(CA3198500)|CA https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=Y76YdybqUxbFqe/S6HB4CnmXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000021650255&ekey=2199&xpn=EP4251775&kind=A4 https://register.epo.org/application?number=EP21897298 https://permalink.orbit.com/RenderStaticFirstPage?XPN=3tFb8gHpanzjCoOEB2EWlnfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT US |(WO2022/113025)|US|(WO2022/113025)|US (CL2023001495)|NAME=NEGATIVE EMISSIONS MATERIALS, INC. 651 N Broad St, Suite 206 Middletown, New Castle, Delaware 19709, 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COUNTRY=AU|(HK40100255)|NAME=ONC LAWYERS , COUNTRY=HK|(VN98973)|NAME=Vision and Partnership Company Limited|(TH2301002998)|NAME=Mr. Sattayapol Satjadechan Mr. Krittawat Chainapasak|(KR10-2023-0110773)|NAME=KIM, JIN HOI NAME=KIM, TAE HONG|(IL303119)|NAME=SHILON ZUCKERSTEIN & CO. 1 AZRIELI CENTER, ROUND TOWER, 19th FLOOR, TEL AVIV TEL AVIV - YAFO 67021 , COUNTRY=IL|(ID2023/04650)|NAME=Emirsyah Dinar|(CA3198500)|NAME=GOWLING WLG (CANADA) LLP , COUNTRY=CA |(EP4251775)|FR; CA|(US20240002973)|FR; CA|(WO2022/113025)|FR; CA|(WO2022/113025)|FR; CA||||(AEP6001220/2023)|FR; CA|||||||||||||||||(CA3198500)|FR; CA (EP4251775)|NAME=LEY, Jeremy William|NAME=DREISINGER, David|(EP4251775)|NAME=LEY, Jeremy William, CITY=75015 Paris, COUNTRY=FR |NAME=DREISINGER, David, CITY=Delta, British Columbia V4M 2P2, COUNTRY=CA|(US20240002973)|NAME=LEY Jeremy William, CITY=Paris, COUNTRY=FR |NAME=DREISINGER David, CITY=Delta, COUNTRY=CA|(WO2022/113025)|NAME=LEY, Jeremy William 140 Rue de la Croix Nivert 75015 Paris, POSTCODE=75015, COUNTRY=FR |NAME=DREISINGER, David 134 49 Street Delta, British Columbia V4M 2P2, POSTCODE=V4M 2P2, COUNTRY=CA|(WO2022/113025)|NAME=LEY, Jeremy William 140 Rue de la Croix Nivert 75015 Paris, POSTCODE=75015, COUNTRY=FR |NAME=DREISINGER, David 134 49 Street Delta, British Columbia V4M 2P2, POSTCODE=V4M 2P2, COUNTRY=CA|(JP2023553314)|NAME=Ray, Jeremy William|NAME=Dry Singer, David|(CN116802326)|NAME=LAY JEREMY WILLIAM|NAME=DREISINGER, DAVID|(ZA202305467)|NAME=LEY, Jeremy William|NAME=DREISINGER, David|(AEP6001220/2023)|NAME=Jeremy William Ley 140 Rue de la Croix Nivert, 75015 Paris, COUNTRY=FR |NAME=David Dreisinger 134 49 Street, Delta, British Columbia V4M 2P2, COUNTRY=CA|(IN202317042083)|NAME=Ley Jeremy William|NAME=Eisinger David|(AU2021389080)|NAME=LEY, Jeremy William|NAME=DREISINGER, David|(AU2021389080)|NAME=LEY, Jeremy William|NAME=DREISINGER, David|(HK40100255)|NAME=LEY Jeremy William|NAME=DREISINGER David|(VN98973)|NAME=LEY Jeremy William|NAME=DREISINGER David|(CR20230285)|NAME=DREISINGER, David|NAME=LEY, Jeremy William|(CL2023001495)|NAME=LEY, Jeremy William 140 Rue de la Croix Nivert 75015 Paris|NAME=DREISINGER, David 134 49 Street Delta, British Columbia V4M 2P2|(ECSP23046201)|NAME=Industrias Peñalver, S.L|NAME=DREISINGER, David|(PE20231629)|NAME=LEY, Jeremy William|NAME=DREISINGER, David|(TH2301002998)|NAME=Lay Jeremy William|NAME=Dreisinger David|(DOP2023000105)|NAME=JEREMY WILLIAM LEY|NAME=DAVID DREISINGER|(KR10-2023-0110773)|NAME=LEY JEREMY WILLIAM|NAME=DREISINGER DAVID|(CO2023007635)|NAME=LEY, Jeremy William|NAME=DREISINGER, David|(BR112023010037)|NAME=LEY JEREMY WILLIAM|NAME=DREISINGER DAVID|(ID2023/04650)|NAME=DREISINGER David|NAME=LEY Jeremy William|(MX2023006141)|NAME=DREISINGER David|NAME=LEY Jeremy William|(CA3198500)|NAME=LEY, JEREMY WILLIAM, COUNTRY=FR |NAME=DREISINGER, DAVID 134 49 STREET, CITY=DELTA, POSTCODE=V4M 2P2, STATE=B1 , COUNTRY=CA 28 25 Titre: (EP4251775)|Integration of carbon sequestration with selective hydrometallurgical recovery of metal values Résumé: (EP4251775)|Processes are provided in which successive steps of hydrometallurgical value extraction may be carried out using the products of carbon capture and an electrolytic reagent-generating process. The electrolytic process provides an acid leachant and an alkali hydroxide, with the alkali hydroxide then available for use either directly as a precipitant in the hydrometallurgical steps, or available for conversion by carbon capture to an alkali metal carbonate that can in turn be used as the precipitant in the selective hydrometallurgical steps. 79 Abstract gpt-4o-mini no The focus is on hydrometallurgical recovery of metals and carbon capture processes, not on accelerated weathering or mineral carbonation for CO₂ sequestration.
79 CN202111446402 CN202111446402 CN114503957|CN114503957 100084457 CN114503957 B 2024-02-13 [CN114503957B]|CN114503957 A 2022-05-17 [CN114503957] 2021-11-30 2021-11-30 2024-02-13|2022-05-17 (CN114503957B)|2024-02-13 (CN114503957)|2041-11-30 (CN114503957)|Method for cooperatively disposing straws by utilizing insects and minerals (CN114503957)|The invention is applicable to the field of solid waste treatment, carbon sequestration and emission reduction, and provides a method for co-processing straws by utilizing insects and minerals, which comprises the following steps: step 1, washing and drying wheat straws, and crushing the wheat straws to the length of 1mm; 2, five minerals including hydroxyapatite, montmorillonite, ferroferric oxide, ferric oxide and aluminum oxide are fully mixed with the straw according to the proportion of 10% and 30%; step 3, putting starved protaetia brevitarsis larvae into the straw mixture in the step 2, recording the initial weight, keeping the humidity of the straw mixture to be 40%, wrapping the beaker with tinfoil, ventilating through an insertion hole, putting the beaker into a dark artificial climate box, and feeding for 10 days; and 4, picking out the larvae, recording the weight, drying the generated fecula at 40 DEG C, grinding, sieving with a 100-mesh sieve, and detecting. The problem of greenhouse gas emission caused by direct straw returning can be effectively relieved, and a new way for efficient utilization of agricultural waste, carbon sequestration and emission reduction is opened up. INSTITUTE OF ENVIRONMENT & SUSTAINABLE DEVELOPMENT AGRICULTURE CHINESE ACADEMY OF AGRICULTURAL SCIENCES (CN114503957)|INSTITUTE OF ENVIRONMENT & SUSTAINABLE DEVELOPMENT IN AGRICULTURE CHINESE ACADEMY OF AGRICULTURAL SCIENCES ([CN])|(CN114503957)|INSTITUTE OF ENVIRONMENT & SUSTAINABLE DEVELOPMENT IN AGRICULTURE CHINESE ACADEMY OF AGRICULTURAL SCIENCES ([CN]) YANG JIANJUN|FENG YA|LIU YICHEN|LIU JIN (CN114503957)|YANG JIANJUN|FENG YA|LIU YICHEN|LIU JIN|(CN114503957)|YANG JIANJUN|FENG YA|LIU YICHEN|LIU JIN (CN114503957)|CHEN BIN;BEIJING ZHONGCHUANG BOTENG INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) et al.|Reg. Nb: 11636 (CN114503957)|Alkyl carbon, aromatic carbon, and the like characterize lignin, tannins, and the like that are difficult to utilize, i.e., recalcitrant carbon.| (CN114503957)|1. A method for cooperatively disposing straws by utilizing insects and minerals, which is characterized by comprising the following steps:step one: cleaning, drying and crushing the wheat straw to the length of 1mm;step two: mixing the five minerals of hydroxyapatite, montmorillonite, ferroferric oxide, ferric oxide and aluminum oxide with straw in a beaker according to the proportion of 10% and 30%;step three: putting the white star flower scarab larvae subjected to starvation treatment into the straw mixture in the second step, recording the initial weight, keeping the humidity of the straw mixture to be 40%, wrapping the beaker by using tinfoil, enabling the jacks to be breathable, and putting the beaker into a dark artificial climate box for feeding for 10 days;step four: picking up larvae, recording weight, drying produced insect manure at 40 ℃, grinding and sieving with a 100-mesh sieve, and detecting;setting three parallel control groups for each treatment in the second step, wherein the dosage of the wheat straw in each beaker in the second step is 10g, and the addition of each mineral in the second step is the dry weight mass ratio of the mineral to the wheat straw powder;the temperature of the artificial climate box in the third step is 25 ℃, and the relative humidity is 50%;putting five white star flower scarab beetle larvae in each beaker in the third step;the hunger treatment in the third step means that the larvae are put into a container which is covered by only the worm manure and has no food, and are put into a dark artificial climate box for cultivation for 7 days;the method for processing the straw by utilizing the cooperation of the insects and the minerals is adopted, the conversion efficiency of the straw to the straw is up to 86 percent, and the total phosphorus in the obtained straw is 42.06 times and 2.47 times of the total potassium in the wheat straw through feeding and conversion of the white flower scarab larvae; in the treatment of adding 10% of hydroxyapatite, montmorillonite, ferric oxide and alumina minerals, the percentage of water-soluble organic carbon (WSOC) in Organic Carbon (OC) in the worm manure is reduced by 2.71%,0.03%,13.57%,4.44% and 5.89%, respectively.| (CN114503957)|The embodiment of the invention aims to provide a method for cooperatively disposing straws by utilizing insects and minerals, which aims to solve the problem of greenhouse gas emission caused by direct returning of the straws to the field.|The invention is applicable to the field of solid waste treatment, carbon fixation and emission reduction, and provides a method for cooperatively disposing straws by utilizing insects and minerals, which comprises the following steps: step one: cleaning, drying and crushing the wheat straw to the length of 1mm; step two: mixing the five minerals of hydroxyapatite, montmorillonite, ferroferric oxide, ferric oxide and aluminum oxide with straw according to the proportion of 10% and 30%; step three: putting the white star flower scarab larvae subjected to starvation treatment into the straw mixture in the second step, recording the initial weight, keeping the humidity of the straw mixture to be 40%, wrapping the beaker by using tinfoil, enabling the jacks to be breathable, and putting the beaker into a dark artificial climate box for feeding for 10 days; step four: and picking out the larvae, recording the weight, drying the produced insect manure at 40 ℃, grinding and sieving with a 100-mesh sieve, and detecting.| (CN114503957)|MINERAL(100,24)|INSECT(100,14)|STRAW DISPOSITION(100,4)|DARK ARTIFICIAL CLIMATE BOX(75,7)|WHEAT STRAW DOSAGE(70,1)|WHEAT STRAW(65,14)|HYDROXYAPATITE MINERAL(62,3)|WHITE FLOWER SCARAB LARVA(62,1)|SCARAB BEETLE LARVA(58,1)|STRAW HUMIDITY(57,5)|WORM MANURE(50,6)|INSECT COOPERATION(50,1)|SCARAB LARVA(48,12)|BEAKER(44,17)|ARTIFICIAL CLIMATE BOX(42,2)|WHITE STAR FLOWER(40,13)|STRAW(38,28)|STARVATION TREATMENT(37,5)|WHEAT STRAW POWDER(37,4)|FERROFERRIC OXIDE(36,6)|ALUMINA MINERAL(36,1)|DRYING PRODUCED INSECT MANURE(35,1)|STRAW RETURNING(31,2)|MONTMORILLONITE(30,11)|PRODUCED INSECT MANURE(29,2)|RECALCITRANT CARBON(29,1)|HUNGER TREATMENT(28,2)|PROCESSING STRAW(27,1)|JACK(26,3)|ARTIFICIAL CLIMATE BOX TEMPERATURE(26,2)|LARVA(23,8)|TINFOIL(23,5)|TOTAL PHOSPHORUS(23,1)|STRAW CONVERSION EFFICIENCY(21,2)|TOTAL POTASSIUM(20,1)|GRINDING(19,5)|CULTIVATION(18,2)|RECORD WEIGHT(18,1)|TANNINS(17,1)|FERRIC OXIDE(16,14)|HYDROXYAPATITE(16,7)|LIGNIN(16,1)|AROMATIC CARBON(15,2)|EMISSION REDUCTION(14,6)|ALUMINUM OXIDE(13,3)|FIXING CARBON(13,2)|PICKING UP LARVA(13,1)|ALKYL CARBON(12,5)|FOOD(12,3)|100 MESH SIEVE(11,5)|GREENHOUSE GAS EMISSION(11,3)|SOLID WASTE TREATMENT(11,2)|STEP FOUR(11,2)|PROTAETIA BREVITARSIS LARVA(11,1)|CARBON FIXATION(10,3)|INSECT MANURE DETECTION(9,2)|MICROBIOLOGICALLY DENSE HINDGUT(9,1)|CONVERSION EFFICIENCY(8,3)|COLEOPTERAN SOIL BORNE INSECT(8,1)|INSECT MANURE NMR CHART(8,1)|SOLID WASTE(7,2)|FERROFERRIC OXIDE MANURE(7,1)|MICROORGANISM MINERALIZATION(7,1)|STRAW DAILY INTAKE(7,1)|WHEAT STRAW CONSUMPTION(7,1)|STEP THREE(6,3)|CPMAS NMR DETECTION(6,2)|DRY WEIGHT MASS RATIO(6,2)|ELEMENTAL ANALYZER(6,2)|WEIGHT MASS RATIO(6,2)|COOPERATIVELY TREATING STRAW(6,1)|COPROCESSING STRAW(6,1)|INSECT MANURE TREATMENT(6,1)|STRAW RESIDUE UTILIZATION(6,1)|TOTAL POTASSIUM TIME(6,1)|WORM DROPPINGS(6,1)|RELATIVE HUMIDITY(5,4)|COTREATING STRAW(5,1)|INTESTINAL MICROORGANISM(5,1)|PBL INTESTINE(5,1)|SOIL DWELLING INVERTEBRATE(5,1)|SOIL RESPIRATION(5,1)|WHITE STAR FLOWER TRANSFORMATION(5,1)|ORGANIC CARBON(4,26)|CARBOXYL CARBON(4,2)|ALKALINE DIGESTIVE JUICE(4,1)|CATION BRIDGING(4,1)|CCPMS NMR(4,1)|CHAFER SPECIES(4,1)|COORDINATION EXCHANGE MODE(4,1)|CRUSHED STRAW(4,1)|EDIBLE PROTEIN(4,1)|ELEMENTAL MEASUREMENT(4,1)|GLOBAL STATE(4,1)|GROUND MINERAL(4,1)|INSECT MANURE ED DIAGRAM(4,1)|MIDDLE INTESTINE(4,1)|MINERAL PROCESSED INSECT MICROSTRUCTURE(4,1)|SFM CARBON SEQUESTRATION(4,1)|STRAW FEEDING(4,1)|TREATED INSECT(4,1)|WHITE STAR SCARAB(4,1)|DIGESTION(3,2)|REMAINING PARAMETER(3,2)|ROTOR DIAMETER(3,2)|TEST PARAMETER(3,2)|TREATMENT CONVERSION(3,2)|ANALOG CONTROL GROUP(3,1)|CARBON NEUTRALIZATION CARBON PEAK(3,1)|DIFFICULT MINERALIZATION(3,1)|FERRIC OXIDE TREATED MANURE(3,1)|IRON PLAY(3,1)|LAND ANIMAL(3,1)|NMR MAIN PEAK(3,1)|NUTRIENT RICH ORGANIC FERTILIZER(3,1)|SOIL ABILITY(3,1)|SOIL GREENHOUSE GAS(3,1)|STRAW TREATMENT POTENTIAL(3,1)|ALUMINA(2,3)|SCANNING ELECTRON MICROSCOPE(2,3)|FECES(2,2)||(CN114503957)|MINERAL(100,29)|INSECT(100,16)|COOPERATIVELY TREATING STRAW(100,6)|HUNGRY SCARAB LARVA(100,3)|TREATING STRAW(100,1)|PLATY STERNON LEUCOCEPHALA LARVA(72,1)|DARK ARTIFICIAL CLIMATE BOX(60,5)|HYDROXYAPATITE MINERAL(54,3)|STRAW HUMIDITY(50,4)|WHEAT STRAW(43,12)|BEAKER(39,19)|PRODUCED INSECT FECES(35,3)|COPROCESSING STRAW(34,3)|FERROFERRIC OXIDE(29,7)|RECORDING PANEL(29,3)|STRAW(26,25)|CODISPOSING STRAW(26,1)|STRAW RETURNING(23,3)|WHEAT STRAW POWDER(21,4)|MONTMORILLONITE(19,10)|TINFOIL(19,5)|VENTILATION(19,5)|GRINDING(16,5)|SCARABAEUS BREVITARSIS HUNGRY LARVA(14,1)|STARVATION TREATMENT(13,3)|FERRIC OXIDE(11,8)|DRY PANEL(11,1)|PICKING OUT LARVA(10,3)|100 MESH SIEVE(9,5)|PLATYSTERNON MEGACEPHALUM LARVA(9,2)|SOLID WASTE TREATMENT(9,2)|STEP FOUR(9,2)|WHEAT STRAW INSECT MANURE(9,1)|ALUMINUM OXIDE(8,6)|EMISSION REDUCTION(8,6)|CARBON FIXATION(8,4)|GREENHOUSE GAS EMISSION(8,4)|WORM MANURE(8,3)|FERROFERRIC OXIDE EXCREMENT(8,2)|SCARAB BEETLE LARVA(8,2)|CLIMATIC CHAMBER(8,1)|WHEAT STRAW INSECT FECES(8,1)|DARK ARTIFICIAL CLIMATE(7,2)|INSECT MANURE DETECTION(7,2)|TREATED INSECT EXCRETA(7,2)|STEP THREE(6,4)|SOLID WASTE(6,2)|GLOBAL LAND ECOSYSTEM(6,1)|INSECT FECES NMR SPECTRUM(6,1)|STEPHANIA MACRANTHOIDE(6,1)|CPMAS NMR(5,3)|CARBON FIXATION FIELD(5,2)|ELEMENTAL ANALYZER(5,2)|FOOD(5,2)|MINERAL TREATED INSECT MICROSTRUCTURE(5,2)|INTESTINAL MICROBE(5,1)|PEST FECES(5,1)|STARVATION TREATED LARVA(5,1)|PERCENTAGE CONTENT(4,5)|AGRICULTURAL CARBON REACHING(4,1)|ALKALINE DIGESTIVE JUICE(4,1)|ATMOSPHERIC CO2THE(4,1)|CATION BRIDGING(4,1)|CRUSHED STRAW(4,1)|HARDLY DECOMPOSED CARBON(4,1)|HCLO4THE DIGESTION(4,1)|INSECT DUNG(4,1)|INSECT FECES ED IMAGE(4,1)|LARVA CONVERSION(4,1)|MICROORGANISM DENSE HINDGUT(4,1)|MINERALSINITIAL PANEL(4,1)|ONLY INSECT FECES(4,1)|PBL INTESTINE(4,1)|RICH NUTRITION(4,1)|SCARAB SPECIES(4,1)|SOIL BORNE INSECT(4,1)|SOIL LIVING INVERTEBRATE(4,1)|STRAW MOISTURE(4,1)|STRAWSTHE DECOMPOSITION(4,1)|WORM EXCREMENT(4,1)|RELATIVE HUMIDITY(3,4)|CARBOXYL CARBON(3,2)|ALKYL CARBON CHARACTERIZATION(3,1)|ATMOSPHERE2THE(3,1)|COORDINATION EXCHANGE(3,1)|DIFFICULT MICROBIAL DEGRADATION(3,1)|EDIBLE PROTEIN(3,1)|EXCREMENT POWDER(3,1)|FEEDING LARVA(3,1)|GROUND MINERAL(3,1)|MIDDLE INTESTINE(3,1)|MIXING HYDROXYAPATITE(3,1)|SFM CARBON SEQUESTRATION(3,1)|TECHNICAL PROPOSAL(3,1)|TREATMENT FECES(3,1)|TEST PARAMETER(2,2)|TREATMENT CONVERSION(2,2)|ARTIFICIAL CLIMATE BOX TEMPERATURE(2,1)|CARBON COMPONENT MINERALIZATION(2,1)|CARBON NEUTRALIZATION(2,1)|DIFFICULT MINERALIZATION(2,1)|FERRIC OXIDE TREATED MANURE(2,1)|IRON PLAY(2,1)|LAND ANIMAL(2,1)|MANURE TREATMENT(2,1)|NMR MAIN PEAK(2,1)|SOIL ABILITY(2,1)|STRAW TREATMENT POTENTIAL(2,1)| (CN114503957)|1. A method for cooperatively disposing straws by utilizing insects and minerals, which is characterized by comprising the following steps:|step one: cleaning, drying and crushing the wheat straw to the length of 1mm;|step two: mixing the five minerals of hydroxyapatite, montmorillonite, ferroferric oxide, ferric oxide and aluminum oxide with straw in a beaker according to the proportion of 10% and 30%;|step three: putting the white star flower scarab larvae subjected to starvation treatment into the straw mixture in the second step, recording the initial weight, keeping the humidity of the straw mixture to be 40%, wrapping the beaker by using tinfoil, enabling the jacks to be breathable, and putting the beaker into a dark artificial climate box for feeding for 10 days;|step four: picking up larvae, recording weight, drying produced insect manure at 40 ℃, grinding and sieving with a 100-mesh sieve, and detecting;|setting three parallel control groups for each treatment in the second step, wherein the dosage of the wheat straw in each beaker in the second step is 10g, and the addition of each mineral in the second step is the dry weight mass ratio of the mineral to the wheat straw powder;|the temperature of the artificial climate box in the third step is 25 ℃, and the relative humidity is 50%;|putting five white star flower scarab beetle larvae in each beaker in the third step;|the hunger treatment in the third step means that the larvae are put into a container which is covered by only the worm manure and has no food, and are put into a dark artificial climate box for cultivation for 7 days;|the method for processing the straw by utilizing the cooperation of the insects and the minerals is adopted, the conversion efficiency of the straw to the straw is up to 86 percent, and the total phosphorus in the obtained straw is 42.06 times and 2.47 times of the total potassium in the wheat straw through feeding and conversion of the white flower scarab larvae; in the treatment of adding 10% of hydroxyapatite, montmorillonite, ferric oxide and alumina minerals, the percentage of water-soluble organic carbon (WSOC) in Organic Carbon (OC) in the worm manure is reduced by 2.71%,0.03%,13.57%,4.44% and 5.89%, respectively. (CN114503957)|TECHNICAL FIELD|[0001] The invention belongs to the field of carbon fixation and emission reduction in solid waste treatment, and particularly relates to a method for cooperatively treating straws by utilizing insects and minerals.|BACKGROUND ART|[0002] Researches show that the straw can directly return to the field to influence the composition and the function of microbial communities, promote the respiration of soil and the decomposition and mineralization of microorganisms on organic matters of the soil and easily mineralized organic carbon components in the straw, and accelerate the emission of greenhouse gases of the soil. The soil organic carbon bank is used as the largest carbon bank in the global land ecological system, and small changes of the soil organic carbon bank can lead to CO in the atmosphere 2 The concentration fluctuates greatly. Thus, the ability of the soil to fix carbon determines to a large extent the CO in the atmosphere 2 Is a concentration of (3).|[0003] In recent years, research has found that soil-dwelling invertebrates, including earthworms and chafer species, can effectively convert various Organic Matters (OM) into nutrient-rich Organic fertilizers and edible proteins, and are an environment-friendly efficient straw waste utilization method. White star scarab (Protaetia brevitarsis, PB) is a common coleopteran soil-borne insect. The larvae (Protaetia brevitarsis larvae, PBL) take OM as food, and the feed comprises humus, crushed straw, sawdust and the like, the straw daily intake amount can reach 0.57g, the conversion efficiency from straw to worm manure is up to 86%, and the worm bodies can be used as medicinal materials or feeds and are commercially cultivated at present to produce high-quality organic fertilizers. Straw is digested by PBL, OM is broken down into a digestible state, dissolved in the PBL intestine by alkaline digestive juice, further enzymatically hydrolyzed in the middle intestine, further fermented in the microbiologically dense hindgut, and the residue and persistent OM are reprecipitated and excreted. Thus, most of the OM that is biodegradable by microorganisms is digested and absorbed by the PBL and intestinal microorganisms together. After minerals are added into the straw, the straw ingested by PBL interacts with the minerals in the digestion process of the straw, and the organic-mineral composite is formed by conversion (the mineral combined organic carbon refers to organic carbon fixed by the minerals in the modes of coordination exchange, cation bridging and the like, and has the characteristics of strong stability, difficult degradation by microorganisms and difficult mineralization), so that the effect of carbon fixation is achieved. Therefore, we propose a carbon sequestration and emission reduction technology (SFM carbon sequestration and emission reduction technology for short) based on a Straw (Straw) -soil animal (Fauna) -soil Mineral (Mineral) system, which provides theoretical basis and technical support for realizing agricultural carbon neutralization carbon peak and even carbon profit.|DISCLOSURE|Disclosure of Invention|[0004] The embodiment of the invention aims to provide a method for cooperatively disposing straws by utilizing insects and minerals, which aims to solve the problem of greenhouse gas emission caused by direct returning of the straws to the field.|[0005] The embodiment of the invention is realized in such a way that the method for cooperatively treating the straws by utilizing the insects and the minerals comprises the following steps:|[0006] step one: cleaning, drying and crushing the wheat straw to about 1mm in length;|[0007] step two: mixing the five minerals of hydroxyapatite, montmorillonite, ferroferric oxide, ferric oxide and aluminum oxide with straw in a beaker according to the proportion of 10% and 30%, and setting three parallel control groups for each treatment;|[0008] step three: putting the white star flower scarab larvae subjected to starvation treatment into the straw mixture in the second step, recording the initial weight, keeping the humidity of the straw mixture to be 40%, wrapping the beaker by using tinfoil, enabling the jacks to be breathable, and putting the beaker into a dark artificial climate box for feeding for 10 days;|[0009] step four: and picking out the larvae, recording the weight, drying the produced insect manure at 40 ℃, grinding and sieving with a 100-mesh sieve, and detecting.|[0010] According to a further technical scheme, the consumption of the wheat straw in each beaker in the second step is 10g.|[0011] According to a further technical scheme, the addition amount of each mineral in the second step is the dry weight mass ratio of the mineral to the wheat straw powder.|[0012] According to a further technical scheme, the temperature of the artificial climate box in the third step is 25 ℃, and the relative humidity is 50%.|[0013] In a further technical scheme, five white star flower scarab larvae are placed in each beaker in the third step.|[0014] According to a further technical scheme, the hunger treatment in the third step is to place the larvae in a container which is covered by only the worm manure and has no food, and place the larvae in a dark artificial climate box for 7 days for cultivation.|[0015] According to the method for cooperatively disposing the straw by utilizing the insects and the minerals, provided by the embodiment of the invention, the straw and the mineral mixture is fed and converted by the white star flower scarab larvae, the relative content of stable organic carbon in the obtained insect manure is higher than that of the straw, and the problem of greenhouse gas emission caused by direct returning of the straw to the field can be effectively relieved.|[0016] The white star flower scarab larvae used in the invention have higher straw conversion efficiency, the straw feeding amount per day is 0.57g, and the conversion efficiency from straw to insect manure is up to 86%. The insect body is rich in high protein, and can be used as medicinal material or feed. The white star flower scarab larvae are easy to raise, the larva period is up to 125-142 days, and the white star flower scarab larvae have higher straw treatment potential.|[0017] The invention uses crop straws such as wheat and the like as raw materials, has large yield, low cost and simple preparation process, and opens up a new way for efficiently utilizing agricultural wastes, fixing carbon and reducing emission.|DRAWINGS DESCRIPTION|[0018] FIG. 1 is an NMR chart of the insect manure obtained by different treatment conversions of a method for co-processing straw by using insects and minerals according to an embodiment of the present invention;|[0019] fig. 2 is an SEM and EDS diagram of the insect manure obtained by different treatment conversions in the method for co-treating straw with insects and minerals according to the embodiment of the present invention.|INVENTION MODE|Detailed Description|[0020] The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0021] Specific implementations of the invention are described in detail below in connection with specific embodiments.|[0022] Example 1:|[0023] production and detection of insect manure|[0024] The wheat straw is cleaned, dried and crushed to a length of about 1 mm. 10g of wheat straw powder was weighed into a beaker. Hydroxyapatite (HAP), montmorillonite (MMT), and ferroferric oxide (Fe) 3 O 4 ) Ferric oxide (Fe) 2 O 3 ) Alumina (Al) 2 O 3 ) Five minerals were thoroughly mixed with straw at a weight ratio of 10% and 30%, 3 parallel per treatment. 5 white star flower scarab larvae which record the initial weight and are subjected to starvation treatment are respectively put into the mixture of the straw and the minerals. The humidity of the straw mixture was kept at 40%. Wrapping the beaker with tinfoil, ventilating the holes, and placing the beaker into a dark artificial climate box at 25 ℃ with relative humidity of 50% for feeding. After 10 days of feeding, the larvae were picked out and weights were recorded. Drying the insect manure produced by each treatment at 40 ℃, grinding and sieving the insect manure with a 100-mesh sieve. Sample ofThe details of the treatment are shown in Table 1.|[0025] Further measuring the content of water-soluble organic carbon (WSOC) and the content of Organic Carbon (OC) as well as the content of K, P and other elements of the insect manure obtained in the example: the OC, TN content was analyzed using an elemental analyzer (Hanau, germany) by selecting an appropriate amount of worm manure passing through a 100 mesh screen. The content of water-soluble organic carbon (WSOC) in the insect manure is 0.034mol L -1 1K 2 SO 4 Extraction (1:5 w/v) was performed and measured with TOC.|[0026] Further characterizing the morphology and the relative content of organic carbon in different treated worm droppings by 13C CPMAS NMR; the microstructure of the mineral-treated worm-feces powder is characterized by a scanning electron microscope and an energy spectrum. In the above measurement method, the test parameters at the time of 13C CPMAS NMR detection are as follows: the rotor diameter was 4mm, the resonance frequency was 125.8MHz, the contact time was 2ms, the cyclic delay time was 2.5s, the number of scans was 6000, and the remaining parameters were automatically set with reference to the machine.|[0027] TABLE 1 sample treatment details including mineral type and amount|[0028] |[0029] Comparative example 1:|[0030] (1) Production and detection of insect manure|[0031] The wheat straw is cleaned, dried and crushed to a length of about 1 mm. 10g of wheat straw powder was weighed into a beaker and 3 parallel were set. 5 white star flower scarab larvae which record the initial weight and are subjected to starvation treatment are respectively put into the straws. The humidity of the straw is kept to be 40 percent. Wrapping the beaker with tinfoil, ventilating the holes, and feeding in a dark artificial climate box at 25deg.C with relative humidity of 50%. After 10 days of feeding, the larvae were picked out and weights were recorded. Drying the insect manure produced by each treatment at 40 ℃, grinding and sieving the insect manure with a 100-mesh sieve.|[0032] Further water-soluble organic carbon (WSOC) content, OC content measurement and K, P and other element measurement are carried out on the insect manure obtained in the comparative example: selecting proper amount of insect manure passing through 100 mesh sieve, passing through 0.034mol L -1 K 2 SO 4 Extraction of WSOC (1:5 w/v) and determination with TOC; the content of OC, TN was analyzed using an elemental analyzer (Hanau, germany); the worm manure is treated by HNO 3 :HClO 4 Digestion was performed with mixed acid=3:1, and elemental measurement was performed with ICP-OES (Agilent 5000). And further characterizing the organic carbon form and the relative content of the organic carbon in different treated insect manure by 13 CCPMS NMR; the microstructure of the mineral-treated worm-feces powder is characterized by a scanning electron microscope and an energy spectrum. In the above measurement method, the test parameters at the time of 13C CPMAS NMR detection are as follows: the rotor diameter was 4mm, the resonance frequency was 125.8MHz, the contact time was 2ms, the cyclic delay time was 2.5s, the number of scans was 6000, and the remaining parameters were automatically set with reference to the machine.|[0033] The total P and total K content of the nutrient elements in the wheat straw and the wheat straw worm manure are shown in Table 2.|[0034] TABLE 2 content of nutrient elements P and K in wheat straw and wheat straw worm feces|[0035] |[0036] As can be seen from the data in Table 2, the total P in the obtained insect manure is 42.06 times and 2.47 times of the total K in the wheat straw after feeding and transformation of the white star flower scarab larvae. Therefore, compared with wheat straw, the insect manure has higher nutrient content, and is a high-quality organic fertilizer.|[0037] The OC, the WSOC values and the ratio of WSOC in the produced manure under different treatments are shown in Table 3.|[0038] TABLE 3 value of OC, WSOC and ratio of WSOC in OC in different treatments of insect manure|[0039] |[0040] Note that: hydroxyapatite (HAP), montmorillonite (MMT), ferroferric oxide (Fe) 3 O 4 ) Ferric oxide (Fe) 2 O 3 ) Alumina (Al) 2 O 3 )|[0041] From the data in table 3, it can be seen that the addition of minerals reduced the OC and WSOC content in the worm manure and the percentage of WSOC in the OC. WSOC in the worm manure was reduced by 19.18%,5.95%,33.63%,18.81% and 20.25% in the treatment with 10% mineral, respectively, compared to the control. In the treatment with 30% mineral addition, the WSOC in the faeces was reduced by 49.51%,29.56%,35.89%,41.97% and 43.55%, respectively. The percentage of WSOC in OC in the worm-feces was reduced by 2.71%,0.03%,13.57%,4.44% and 5.89%, respectively, in the treatment with 10% mineral compared to the control. In the treatment of adding 30% of minerals, the percentage of WSOC in OC in the insect manure is reduced by 5.58%,2.80%,3.32%,3.86% and 4.26% of water-soluble organic carbon are regarded as being composed of unstable organic carbon compounds, so that the type and the amount of the minerals with the best carbon fixing effect are determined to be 10% of ferric oxide, and the percentage of the WSOC in the OC in the insect manure can be reduced to the greatest extent.|[0042] To verify the effect of mineral processing on the chemical structure of organic carbon in the manure in the method of the invention, 13C CPMAS NMR was used to detect changes in the chemical structure of organic carbon in the manure.|[0043] As can be seen from fig. 1 in combination with the data in table 4:|[0044] the chemical shift ranges 0 to 45ppm,45 to 110ppm,110 to 140ppm,140 to 160ppm and 160 to 220ppm are alkyl carbon, O/N-alkyl carbon, C-substituted aromatic carbon, O-substituted aromatic carbon and carboxyl carbon, respectively. The NMR main peaks and the maximum signal intensity of all the worm droppings are in the O/N-alkyl carbon region, and then alkyl carbon, C substituted aromatic carbon and carboxyl carbon are the second, and the content of the O substituted aromatic carbon is the smallest. Alkyl carbon, aromatic carbon, and the like characterize lignin, tannins, and the like that are difficult to utilize, i.e., recalcitrant carbon. The results in Table 4 show that the alkyl carbon content in the manure is significantly increased after the mineral addition. The percentage of alkyl carbon in the ferric oxide and the ferric oxide manure in the 10% treatment is increased by 19% and 22% respectively compared with the control. The percentage of alkyl carbon in the montmorillonite and the ferroferric oxide manure in the 30 percent treatment is respectively increased by 22 percent and 29.7 percent. In addition, the aromatic carbon content in 10% ferric oxide and 30% ferric oxide is significantly improved by 59.8% and 41.4%. Studies have shown that iron plays an important role in the accumulation of organic carbon in the soil, and that iron participates in physical, chemical and biological protection mechanisms by promoting the formation of agglomerates, co-precipitation and adsorption with organic carbon, and affecting microbial activity, respectively.|[0045] TABLE 4 relative content of organic carbon in insect manure|[0046] |[0047] Note that: hydroxyapatite (HAP), montmorillonite (MMT), ferroferric oxide (Fe) 3 O 4 ) Ferric oxide (Fe) 2 O 3 ) Alumina (Al) 2 O 3 )|[0048] In order to more vividly verify the influence of mineral treatment on the chemical structure of organic carbon in the insect manure, the combination mode of minerals and organic carbon in the insect manure is characterized by combining STM with EDS.|[0049] From the data in fig. 2, it can be seen that:|[0050] the image of the scanning electron microscope shows the microstructure of the mineral-processed insect manure powder, and the added mineral particles tightly wrap the organic matters (such as straw) in the insect manure to form mineral-combined organic matters, so that the decomposition of the organic matters in the intestinal tracts of the white star flower scarab larvae is greatly reduced, and the data of OC and WSOC are consistent. EDS results showed that 10% ferric oxide treated manure had the highest carbon content.|[0051] Considering the price and the use amount of minerals and the carbon fixing effect thereof, 10% ferric oxide treatment is preferable as the optimal addition.|[0052] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention. (CN114503957)|TECHNICAL FIELD|[0001] The invention belongs to the field of carbon fixation and emission reduction in solid waste treatment, and particularly relates to a method for cooperatively treating straws by utilizing insects and minerals.|BACKGROUND ART|[0002] Researches show that the straw can directly return to the field to influence the composition and the function of microbial communities, promote the respiration of soil and the decomposition and mineralization of microorganisms on organic matters of the soil and easily mineralized organic carbon components in the straw, and accelerate the emission of greenhouse gases of the soil. The soil organic carbon bank is used as the largest carbon bank in the global land ecological system, and small changes of the soil organic carbon bank can lead to CO in the atmosphere 2 The concentration fluctuates greatly. Thus, the ability of the soil to fix carbon determines to a large extent the CO in the atmosphere 2 Is a concentration of (3).|[0003] In recent years, research has found that soil-dwelling invertebrates, including earthworms and chafer species, can effectively convert various Organic Matters (OM) into nutrient-rich Organic fertilizers and edible proteins, and are an environment-friendly efficient straw waste utilization method. White star scarab (Protaetia brevitarsis, PB) is a common coleopteran soil-borne insect. The larvae (Protaetia brevitarsis larvae, PBL) take OM as food, and the feed comprises humus, crushed straw, sawdust and the like, the straw daily intake amount can reach 0.57g, the conversion efficiency from straw to worm manure is up to 86%, and the worm bodies can be used as medicinal materials or feeds and are commercially cultivated at present to produce high-quality organic fertilizers. Straw is digested by PBL, OM is broken down into a digestible state, dissolved in the PBL intestine by alkaline digestive juice, further enzymatically hydrolyzed in the middle intestine, further fermented in the microbiologically dense hindgut, and the residue and persistent OM are reprecipitated and excreted. Thus, most of the OM that is biodegradable by microorganisms is digested and absorbed by the PBL and intestinal microorganisms together. After minerals are added into the straw, the straw ingested by PBL interacts with the minerals in the digestion process of the straw, and the organic-mineral composite is formed by conversion (the mineral combined organic carbon refers to organic carbon fixed by the minerals in the modes of coordination exchange, cation bridging and the like, and has the characteristics of strong stability, difficult degradation by microorganisms and difficult mineralization), so that the effect of carbon fixation is achieved. Therefore, we propose a carbon sequestration and emission reduction technology (SFM carbon sequestration and emission reduction technology for short) based on a Straw (Straw) -soil animal (Fauna) -soil Mineral (Mineral) system, which provides theoretical basis and technical support for realizing agricultural carbon neutralization carbon peak and even carbon profit.|DISCLOSURE|Disclosure of Invention|[0004] The embodiment of the invention aims to provide a method for cooperatively disposing straws by utilizing insects and minerals, which aims to solve the problem of greenhouse gas emission caused by direct returning of the straws to the field.|[0005] The embodiment of the invention is realized in such a way that the method for cooperatively treating the straws by utilizing the insects and the minerals comprises the following steps:|[0006] step one: cleaning, drying and crushing the wheat straw to about 1mm in length;|[0007] step two: mixing the five minerals of hydroxyapatite, montmorillonite, ferroferric oxide, ferric oxide and aluminum oxide with straw in a beaker according to the proportion of 10% and 30%, and setting three parallel control groups for each treatment;|[0008] step three: putting the white star flower scarab larvae subjected to starvation treatment into the straw mixture in the second step, recording the initial weight, keeping the humidity of the straw mixture to be 40%, wrapping the beaker by using tinfoil, enabling the jacks to be breathable, and putting the beaker into a dark artificial climate box for feeding for 10 days;|[0009] step four: and picking out the larvae, recording the weight, drying the produced insect manure at 40 ℃, grinding and sieving with a 100-mesh sieve, and detecting.|[0010] According to a further technical scheme, the consumption of the wheat straw in each beaker in the second step is 10g.|[0011] According to a further technical scheme, the addition amount of each mineral in the second step is the dry weight mass ratio of the mineral to the wheat straw powder.|[0012] According to a further technical scheme, the temperature of the artificial climate box in the third step is 25 ℃, and the relative humidity is 50%.|[0013] In a further technical scheme, five white star flower scarab larvae are placed in each beaker in the third step.|[0014] According to a further technical scheme, the hunger treatment in the third step is to place the larvae in a container which is covered by only the worm manure and has no food, and place the larvae in a dark artificial climate box for 7 days for cultivation.|[0015] According to the method for cooperatively disposing the straw by utilizing the insects and the minerals, provided by the embodiment of the invention, the straw and the mineral mixture is fed and converted by the white star flower scarab larvae, the relative content of stable organic carbon in the obtained insect manure is higher than that of the straw, and the problem of greenhouse gas emission caused by direct returning of the straw to the field can be effectively relieved.|[0016] The white star flower scarab larvae used in the invention have higher straw conversion efficiency, the straw feeding amount per day is 0.57g, and the conversion efficiency from straw to insect manure is up to 86%. The insect body is rich in high protein, and can be used as medicinal material or feed. The white star flower scarab larvae are easy to raise, the larva period is up to 125-142 days, and the white star flower scarab larvae have higher straw treatment potential.|[0017] The invention uses crop straws such as wheat and the like as raw materials, has large yield, low cost and simple preparation process, and opens up a new way for efficiently utilizing agricultural wastes, fixing carbon and reducing emission.|DRAWINGS DESCRIPTION|[0018] FIG. 1 is an NMR chart of the insect manure obtained by different treatment conversions of a method for co-processing straw by using insects and minerals according to an embodiment of the present invention;|[0019] fig. 2 is an SEM and EDS diagram of the insect manure obtained by different treatment conversions in the method for co-treating straw with insects and minerals according to the embodiment of the present invention.|INVENTION MODE|Detailed Description|[0020] The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0021] Specific implementations of the invention are described in detail below in connection with specific embodiments.|[0022] Example 1:|[0023] production and detection of insect manure|[0024] The wheat straw is cleaned, dried and crushed to a length of about 1 mm. 10g of wheat straw powder was weighed into a beaker. Hydroxyapatite (HAP), montmorillonite (MMT), and ferroferric oxide (Fe) 3 O 4 ) Ferric oxide (Fe) 2 O 3 ) Alumina (Al) 2 O 3 ) Five minerals were thoroughly mixed with straw at a weight ratio of 10% and 30%, 3 parallel per treatment. 5 white star flower scarab larvae which record the initial weight and are subjected to starvation treatment are respectively put into the mixture of the straw and the minerals. The humidity of the straw mixture was kept at 40%. Wrapping the beaker with tinfoil, ventilating the holes, and placing the beaker into a dark artificial climate box at 25 ℃ with relative humidity of 50% for feeding. After 10 days of feeding, the larvae were picked out and weights were recorded. Drying the insect manure produced by each treatment at 40 ℃, grinding and sieving the insect manure with a 100-mesh sieve. Sample ofThe details of the treatment are shown in Table 1.|[0025] Further measuring the content of water-soluble organic carbon (WSOC) and the content of Organic Carbon (OC) as well as the content of K, P and other elements of the insect manure obtained in the example: the OC, TN content was analyzed using an elemental analyzer (Hanau, germany) by selecting an appropriate amount of worm manure passing through a 100 mesh screen. The content of water-soluble organic carbon (WSOC) in the insect manure is 0.034mol L -1 1K 2 SO 4 Extraction (1:5 w/v) was performed and measured with TOC.|[0026] Further characterizing the morphology and the relative content of organic carbon in different treated worm droppings by 13C CPMAS NMR; the microstructure of the mineral-treated worm-feces powder is characterized by a scanning electron microscope and an energy spectrum. In the above measurement method, the test parameters at the time of 13C CPMAS NMR detection are as follows: the rotor diameter was 4mm, the resonance frequency was 125.8MHz, the contact time was 2ms, the cyclic delay time was 2.5s, the number of scans was 6000, and the remaining parameters were automatically set with reference to the machine.|[0027] TABLE 1 sample treatment details including mineral type and amount|[0028] |[0029] Comparative example 1:|[0030] (1) Production and detection of insect manure|[0031] The wheat straw is cleaned, dried and crushed to a length of about 1 mm. 10g of wheat straw powder was weighed into a beaker and 3 parallel were set. 5 white star flower scarab larvae which record the initial weight and are subjected to starvation treatment are respectively put into the straws. The humidity of the straw is kept to be 40 percent. Wrapping the beaker with tinfoil, ventilating the holes, and feeding in a dark artificial climate box at 25deg.C with relative humidity of 50%. After 10 days of feeding, the larvae were picked out and weights were recorded. Drying the insect manure produced by each treatment at 40 ℃, grinding and sieving the insect manure with a 100-mesh sieve.|[0032] Further water-soluble organic carbon (WSOC) content, OC content measurement and K, P and other element measurement are carried out on the insect manure obtained in the comparative example: selecting proper amount of insect manure passing through 100 mesh sieve, passing through 0.034mol L -1 K 2 SO 4 Extraction of WSOC (1:5 w/v) and determination with TOC; the content of OC, TN was analyzed using an elemental analyzer (Hanau, germany); the worm manure is treated by HNO 3 :HClO 4 Digestion was performed with mixed acid=3:1, and elemental measurement was performed with ICP-OES (Agilent 5000). And further characterizing the organic carbon form and the relative content of the organic carbon in different treated insect manure by 13 CCPMS NMR; the microstructure of the mineral-treated worm-feces powder is characterized by a scanning electron microscope and an energy spectrum. In the above measurement method, the test parameters at the time of 13C CPMAS NMR detection are as follows: the rotor diameter was 4mm, the resonance frequency was 125.8MHz, the contact time was 2ms, the cyclic delay time was 2.5s, the number of scans was 6000, and the remaining parameters were automatically set with reference to the machine.|[0033] The total P and total K content of the nutrient elements in the wheat straw and the wheat straw worm manure are shown in Table 2.|[0034] TABLE 2 content of nutrient elements P and K in wheat straw and wheat straw worm feces|[0035] |[0036] As can be seen from the data in Table 2, the total P in the obtained insect manure is 42.06 times and 2.47 times of the total K in the wheat straw after feeding and transformation of the white star flower scarab larvae. Therefore, compared with wheat straw, the insect manure has higher nutrient content, and is a high-quality organic fertilizer.|[0037] The OC, the WSOC values and the ratio of WSOC in the produced manure under different treatments are shown in Table 3.|[0038] TABLE 3 value of OC, WSOC and ratio of WSOC in OC in different treatments of insect manure|[0039] |[0040] Note that: hydroxyapatite (HAP), montmorillonite (MMT), ferroferric oxide (Fe) 3 O 4 ) Ferric oxide (Fe) 2 O 3 ) Alumina (Al) 2 O 3 )|[0041] From the data in table 3, it can be seen that the addition of minerals reduced the OC and WSOC content in the worm manure and the percentage of WSOC in the OC. WSOC in the worm manure was reduced by 19.18%,5.95%,33.63%,18.81% and 20.25% in the treatment with 10% mineral, respectively, compared to the control. In the treatment with 30% mineral addition, the WSOC in the faeces was reduced by 49.51%,29.56%,35.89%,41.97% and 43.55%, respectively. The percentage of WSOC in OC in the worm-feces was reduced by 2.71%,0.03%,13.57%,4.44% and 5.89%, respectively, in the treatment with 10% mineral compared to the control. In the treatment of adding 30% of minerals, the percentage of WSOC in OC in the insect manure is reduced by 5.58%,2.80%,3.32%,3.86% and 4.26% of water-soluble organic carbon are regarded as being composed of unstable organic carbon compounds, so that the type and the amount of the minerals with the best carbon fixing effect are determined to be 10% of ferric oxide, and the percentage of the WSOC in the OC in the insect manure can be reduced to the greatest extent.|[0042] To verify the effect of mineral processing on the chemical structure of organic carbon in the manure in the method of the invention, 13C CPMAS NMR was used to detect changes in the chemical structure of organic carbon in the manure.|[0043] As can be seen from fig. 1 in combination with the data in table 4:|[0044] the chemical shift ranges 0 to 45ppm,45 to 110ppm,110 to 140ppm,140 to 160ppm and 160 to 220ppm are alkyl carbon, O/N-alkyl carbon, C-substituted aromatic carbon, O-substituted aromatic carbon and carboxyl carbon, respectively. The NMR main peaks and the maximum signal intensity of all the worm droppings are in the O/N-alkyl carbon region, and then alkyl carbon, C substituted aromatic carbon and carboxyl carbon are the second, and the content of the O substituted aromatic carbon is the smallest. Alkyl carbon, aromatic carbon, and the like characterize lignin, tannins, and the like that are difficult to utilize, i.e., recalcitrant carbon. The results in Table 4 show that the alkyl carbon content in the manure is significantly increased after the mineral addition. The percentage of alkyl carbon in the ferric oxide and the ferric oxide manure in the 10% treatment is increased by 19% and 22% respectively compared with the control. The percentage of alkyl carbon in the montmorillonite and the ferroferric oxide manure in the 30 percent treatment is respectively increased by 22 percent and 29.7 percent. In addition, the aromatic carbon content in 10% ferric oxide and 30% ferric oxide is significantly improved by 59.8% and 41.4%. Studies have shown that iron plays an important role in the accumulation of organic carbon in the soil, and that iron participates in physical, chemical and biological protection mechanisms by promoting the formation of agglomerates, co-precipitation and adsorption with organic carbon, and affecting microbial activity, respectively.|[0045] TABLE 4 relative content of organic carbon in insect manure|[0046] |[0047] Note that: hydroxyapatite (HAP), montmorillonite (MMT), ferroferric oxide (Fe) 3 O 4 ) Ferric oxide (Fe) 2 O 3 ) Alumina (Al) 2 O 3 )|[0048] In order to more vividly verify the influence of mineral treatment on the chemical structure of organic carbon in the insect manure, the combination mode of minerals and organic carbon in the insect manure is characterized by combining STM with EDS.|[0049] From the data in fig. 2, it can be seen that:|[0050] the image of the scanning electron microscope shows the microstructure of the mineral-processed insect manure powder, and the added mineral particles tightly wrap the organic matters (such as straw) in the insect manure to form mineral-combined organic matters, so that the decomposition of the organic matters in the intestinal tracts of the white star flower scarab larvae is greatly reduced, and the data of OC and WSOC are consistent. EDS results showed that 10% ferric oxide treated manure had the highest carbon content.|[0051] Considering the price and the use amount of minerals and the carbon fixing effect thereof, 10% ferric oxide treatment is preferable as the optimal addition.|[0052] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention. Family Number|(100084457)|100084457|Abstract|(CN114503957B B)|The invention is applicable to the field of solid waste treatment , carbon sequestration and emission reduction , and provides a method for co - processing straws by utilizing insects and minerals , which comprises the following steps : step 1, washing and drying wheat straws , and crushing the wheat straws to the length of 1 mm ; 2, five minerals including hydroxyapatite , montmorillonite , ferroferric oxide , ferric oxide and aluminum oxide are fully mixed with the straw according to the proportion of 10% and 30% ; step 3, putting starved protaetia brevitarsis larvae into the straw mixture in the step 2, recording the initial weight , keeping the humidity of the straw mixture to be 40%, wrapping the beaker with tinfoil , ventilating through an insertion hole , putting the beaker into a dark artificial climate box , and feeding for 10 days ; and 4, picking out the larvae , recording the weight , drying the generated fecula at 40 DEG C , grinding , sieving with a 100- mesh sieve , and detecting . The problem of greenhouse gas emission caused by direct straw returning can be effectively relieved , and a new way for efficient utilization of agricultural waste , carbon sequestration and emission reduction is opened up . |CPC codes|(CN114503957B B)|A01K - 067/30 |IPC codes|(CN114503957B B)|A01K - 067/033 | Food chemistry|Other special machines A01K-067/30|A23K-010/20|Y02P-060/87 A01K-067/30|A23K-010/20|Y02P-060/87 A01K-067/033|A23K-010/20 A01K-067/033|A23K-010/20 CN112956452|AU2020103489|CN111345268|US20210307360|CN108551796|CN103976153|CN102987076 CN112956452 94720621 WHO=Examiner SELF=N|AU2020103489 92470962 WHO=Examiner SELF=N|CN111345268 89516914 WHO=Examiner SELF=N|US20210307360 86871621 WHO=Examiner SELF=N|CN108551796 81394286 WHO=Examiner SELF=N|CN103976153 67215104 WHO=Examiner SELF=N|CN102987076 44841398 WHO=Examiner SELF=N 寿秀玲 等: &quot;“水稻秸秆施用后土壤溶解性有机碳的变化与土壤CO2排放”&quot;, 《土壤通报》, vol. 48, no. 5, pages 1218 - 1225 (Cat. Y)|刘玉升 等: &quot;“基于白星花金龟幼虫转化玉米秸秆的微循环农牧场模式研究”&quot;, 《安徽农业科学》, vol. 43, no. 31, pages 85 - 87 (Cat. A)|“基于白星花金龟幼虫转化玉米秸秆的微循环农牧场模式研究”;刘玉升 等;《安徽农业科学》;第43卷(第31期);第85-87页 (Cat. A)|“水稻秸秆施用后土壤溶解性有机碳的变化与土壤CO2排放”;寿秀玲 等;《土壤通报》;第48卷(第5期);第1218-1225页 (Cat. Y) CN111345268; US20210307360; CN112956452; CN108551796; AU2020103489; CN102987076; CN103976153 GRANTED (CN114503957)|GRANTED ALIVE (CN114503957)|ALIVE (CN114503957)|LEGAL DETAILS FOR CN114503957|Actual or expected expiration date=2041-11-30|Legal state=ALIVE|Status=GRANTED|Event publication date=2021-11-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202111446402|Application date=2021-11-30|Standardized application number=2021CN-1446402|Event publication date=2022-05-17|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114503957|Publication stage code=A|Publication date=2022-05-17|Standardized publication number=CN114503957|Event publication date=2022-05-17|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-11-25|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-02-13|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN114503957|Publication stage code=B|Publication date=2024-02-13|Standardized publication number=CN114503957B|Event publication date=2024-02-13|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN114503957)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRUZ3SpQlTs4Bj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000071446149&ekey=1846&xpn=CN114503957B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=QU7Q3Mcc67GuQbZm7IfFbbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN114503957)|CN|(CN114503957)|CN (CN114503957)|NAME=INSTITUTE OF ENVIRONMENT & SUSTAINABLE DEVELOPMENT IN AGRICULTURE CHINESE ACADEMY OF AGRICULTURAL SCIENCES , COUNTRY=CN|(CN114503957)|NAME=INSTITUTE OF ENVIRONMENT & SUSTAINABLE DEVELOPMENT IN AGRICULTURE CHINESE ACADEMY OF AGRICULTURAL SCIENCES , COUNTRY=CN (CN114503957)|NAME=CHEN BIN;BEIJING ZHONGCHUANG BOTENG INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) et al. , REG=11636|(CN114503957)|NAME=CHEN BIN;BEIJING ZHONGCHUANG BOTENG INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) et al. , REG=11636 (CN114503957)|NAME=YANG JIANJUN|NAME=FENG YA|NAME=LIU YICHEN|NAME=LIU JIN|(CN114503957)|NAME=YANG JIANJUN|NAME=FENG YA|NAME=LIU YICHEN|NAME=LIU JIN 0 1 Titre: (CN114503957)|Method for cooperatively disposing straws by utilizing insects and minerals Résumé: (CN114503957)|The invention is applicable to the field of solid waste treatment, carbon sequestration and emission reduction, and provides a method for co-processing straws by utilizing insects and minerals, which comprises the following steps: step 1, washing and drying wheat straws, and crushing the wheat straws to the length of 1mm; 2, five minerals including hydroxyapatite, montmorillonite, ferroferric oxide, ferric oxide and aluminum oxide are fully mixed with the straw according to the proportion of 10% and 30%; step 3, putting starved protaetia brevitarsis larvae into the straw mixture in the step 2, recording the initial weight, keeping the humidity of the straw mixture to be 40%, wrapping the beaker with tinfoil, ventilating through an insertion hole, putting the beaker into a dark artificial climate box, and feeding for 10 days; and 4, picking out the larvae, recording the weight, drying the generated fecula at 40 DEG C, grinding, sieving with a 100-mesh sieve, and detecting. The problem of greenhouse gas emission caused by direct straw returning can be effectively relieved, and a new way for efficient utilization of agricultural waste, carbon sequestration and emission reduction is opened up. 76 Abstract gpt-4o-mini no The article focuses on solid waste treatment and the use of insects in processing straws, without a clear emphasis on accelerated weathering of minerals for CO₂ capture.
80 CN201210032120 CN201210032120 CN102583313|CN102583313 7788454 CN102583313 B 2013-10-23 [CN102583313B]|CN102583313 A 2012-07-18 [CN102583313] 2012-02-14 2012-02-14 2013-10-23|2012-07-18 (CN102583313B)|2013-10-23 (CN102583313)|2018-02-14 (CN102583313)|Rural household garbage carbonization method, prepared products using same, and application (CN102583313)|The invention discloses a rural household garbage carbonization method, prepared products using same, and an application. The method comprises steps of sorting household garbage, rejecting inorganic garbage and organic garbage capable of generating toxic hazardous substance through burning, performing natural air drying on the sorted garbage, performing coarse crushing on the sorted garbage to enable the particle diameter of the garbage to be no more than 5 cm, subjecting the garbage after being crushed coarsely to carbonization for a time from 20 minutes to 5 hours at a temperature in a range between 350 DEG C and 500 DEG C under the condition of oxygen deficiency, cooling naturally the garbage, and obtaining the carbonization products. The rural household garbage carbonization method, the prepared products using the same, and the application combine rural household garbage processing, resource application and carbon sequestration and have the advantages of being economic, effective,environment-friendly, easy in operation, and easy to popularize. As fertilizers, the prepared carbonization products improve farmland soil and crop output and cannot generate secondary pollution. ZHEJIANG UNIVERSITY (CN102583313)|ZHEJIANG UNIV|(CN102583313)|ZHEJIANG UNIV WU JIAPING|ZHAO RUDONG (CN102583313)|WU JIAPING|ZHAO RUDONG|(CN102583313)|WU JIAPING|ZHAO RUDONG (CN102583313)|HU HONGJUAN;HANGZHOU TIANQIN INTELLECTUAL PROPERTY AGENCY CO LTD (CN102583313)|The method aims at obtaining the semi-coke type carbon, and has the advantages of complex steps and longer carbonization time.|The method has the advantages of complex flow, more required machine equipment and higher cost.|The increase of carbon dioxide concentration in the atmosphere caused by human activities is the most important source of global climate change, and emission reduction and carbon sequestration have become hot problems related to scientific research and international political, economic and outwork disputes.|The treatment of domestic garbage is a global problem, the garbage is accumulated in large quantity and directly pollutes soil, surface runoff, underground water and the like in a treatment mode mainly by landfill at the present stage, harmful substances, greenhouse gases such as methane and the like are released, and the human health and the environment are greatly threatened.| (CN102583313)|1. A method for carbonizing rural domestic garbage is characterized by comprising the following steps:(1) sorting the rural domestic garbage, and removing inorganic garbage and organic garbage which can generate toxic and harmful substances after incineration;(2) naturally drying the sorted garbage, and then coarsely crushing to ensure that the particle size is less than or equal to 5 cm;(3) carbonizing the coarsely crushed household garbage under an anoxic condition, wherein the carbonization temperature is 350-500 ℃, the carbonization duration is 20 min-5 h, and naturally cooling to obtain a carbonized product;the components of the carbonized product are a mixture of biochar and burned soil.| (CN102583313)|The invention also provides a carbonized product prepared by the method. Further, the invention also provides application of the carbonized product, the carbonized product is scattered in soil, the depth of the carbonized product applied in the soil is 0-20 cm, and the carbonized product is applied independently or matched with a fertilizer.|The invention discloses a method for carbonizing rural domestic garbage, a carbonized product and application thereof, wherein the method comprises the following steps: sorting the household garbage, and removing inorganic garbage and organic garbage which can generate toxic and harmful substances after incineration; naturally drying the sorted garbage in the air, and then coarsely crushing the garbage to ensure that the particle size is less than or equal to 5 cm; carbonizing the coarsely crushed household garbage under an anoxic condition, wherein the carbonization temperature is 350-500 ℃, the carbonization time is 20 min-5 h, and naturally cooling to obtain a carbonized product.|The invention relates to the technical field of rural solid waste recycling, in particular to a method for carbonizing rural domestic garbage, a product and application thereof.| (CN102583313)|RURAL DOMESTIC GARBAGE(100,14)|RURAL HOUSEHOLD GARBAGE(100,1)|COARSELY CRUSHED HOUSEHOLD GARBAGE(98,4)|CARBONIZED PRODUCT(58,37)|HOUSEHOLD GARBAGE(58,7)|SORTED GARBAGE(43,1)|HARMFUL SUBSTANCE(41,6)|OUTWORK DISPUTE(40,1)|INORGANIC GARBAGE(39,4)|TOXIC SUBSTANCE(38,4)|CARBONIZATION DURATION(38,1)|ORGANIC GARBAGE(32,4)|RURAL DOMESTIC GARBAGE TREATMENT(32,2)|INCINERATION(31,2)|ANOXIC CONDITION(28,4)|FERTILIZER(27,13)|BURNED SOIL(26,2)|CHARRED PRODUCT(25,3)|FARMLAND SOIL(25,1)|DOMESTIC GARBAGE(24,4)|CARBONIZATION TEMPERATURE(23,5)|DOMESTIC GARBAGE TREATMENT(19,2)|METHANEDIONE(19,1)|GARBAGE(18,8)|MACHINE EQUIPMENT(17,1)|GROUND(15,14)|LANDFILL(15,1)|CARBON SEQUESTRATION(14,3)|FERTILIZER COMPOUND(14,2)|PREPARED CARBONIZED PRODUCT(14,1)|SOLID WASTE RECYCLING(14,1)|METHANE(13,1)|BIOCHAR(12,5)|CONTAMINATION(11,2)|HUMAN HEALTH(11,1)|GREENHOUSE GAS(10,1)|SORTED DOMESTIC GARBAGE(9,2)|TREATMENT MODE(9,2)|EMISSION REDUCTION(9,1)|HUMAN ACTIVITY(9,1)|COMPLEX FLOW(8,1)|GARBAGE ACCUMULATION EMBARRASSMENT(8,1)|GLOBAL CLIMATE CHANGE SOURCE(8,1)|SEMICOKE TYPE CARBON(8,1)|UNDERGROUND WATER(8,1)|BARREN FARMLAND(7,2)|URBAN DOMESTIC(7,2)|NITROGEN FERTILIZER(6,7)|PARTICLE SIZE(6,5)|CARBONIZATION TIME(6,4)|CROP POTATO(6,2)|YELLOW RIB MUD(6,2)|DAILY DOMESTIC GARBAGE(6,1)|GARBAGE PILE MIDDLE(6,1)|SOLID WASTE(6,1)|CROP YIELD(5,4)|GLOBAL CLIMATE CHANGE(5,2)|CARBONIZED DOMESTIC GARBAGE PRODUCT(5,1)|FARMER FARMLAND(5,1)|REST DOMESTIC GARBAGE(5,1)|UNBALANCED FERTILIZER(5,1)|URBANIZATION ACCELERATION(5,1)|ABSORBING SEWAGE(4,1)|CARBONIZATION FURNACE(4,1)|CARBONIZED PRODUCT COAPPLICATION(4,1)|GARBAGE POOL(4,1)|HOT MELTING CELLAR(4,1)|HOUSEHOLD GARBAGE CARBON CONTENT(4,1)|INCOMPLETE CARBONIZATION(4,1)|LONG CARBONIZATION TIME(4,1)|POULTRY EXCREMENT(4,1)|POULTRY MANURE(4,1)|RECOVERING WASTE IRON(4,1)|REDUCING METHANEDIONE EMISSION(4,1)|REINFORCED CURING SLURRY(4,1)|RETURNING ORGANIC GARBAGE(4,1)|SCIENTIFIC RECYCLING(4,1)|SURFACE RUNOFF(4,1)|TOOTH CHOPPER(4,1)|GROWTH PERIOD(3,3)|STRAW(3,2)|TREATING GARBAGE(3,2)|AGRICULTURAL BENEFIT(3,1)|ANIMAL BONE(3,1)|BIOCHAR CARBON CONTENT(3,1)|CARBONIZATION TREATMENT(3,1)|DUST GARBAGE(3,1)|EXTENSIVE TREATMENT(3,1)|T HM2THE FERTILIZER(3,1)|URBAN ECONOMIC CONSTRUCTION DEVELOPMENT(3,1)|VEGETABLE LEAVE(3,1)|CURING BLOCK(2,2)|FERTILITY(2,2)|LIVESTOCK(2,2)|5T HM2THE(2,1)|AUTOMATIC IRON RECOVERY MACHINE(2,1)|CARBONIZATION CONDITION(2,1)|ECONOMIC BENEFIT(2,1)|QUALITY DEGRADATION(2,1)|QUZHOU REGION(2,1)|SIGNIFICANCE(2,1)||(CN102583313)|RURAL DOMESTIC GARBAGE(100,14)|RURAL HOUSEHOLD GARBAGE(100,1)|COARSELY CRUSHED HOUSEHOLD GARBAGE(98,4)|HOUSEHOLD GARBAGE(58,7)|CARBONIZED PRODUCT(54,35)|SORTED GARBAGE(43,1)|HARMFUL SUBSTANCE(41,6)|OUTWORK DISPUTE(40,1)|INORGANIC GARBAGE(39,4)|TOXIC SUBSTANCE(38,4)|CARBONIZATION DURATION(38,1)|ORGANIC GARBAGE(32,4)|RURAL DOMESTIC GARBAGE TREATMENT(32,2)|INCINERATION(31,2)|ANOXIC CONDITION(28,4)|FERTILIZER(27,13)|FARMLAND SOIL(25,1)|DOMESTIC GARBAGE(24,4)|CARBONIZATION TEMPERATURE(23,5)|CHARRED PRODUCT(23,4)|DOMESTIC GARBAGE TREATMENT(19,2)|METHANEDIONE(19,1)|GARBAGE(18,8)|MACHINE EQUIPMENT(17,1)|GROUND(15,14)|LANDFILL(15,1)|CARBON SEQUESTRATION(14,3)|FERTILIZER COMPOUND(14,2)|PREPARED CARBONIZED PRODUCT(14,1)|SOLID WASTE RECYCLING(14,1)|METHANE(13,1)|CONTAMINATION(11,2)|HUMAN HEALTH(11,1)|GREENHOUSE GAS(10,1)|SORTED DOMESTIC GARBAGE(9,2)|TREATMENT MODE(9,2)|EMISSION REDUCTION(9,1)|HUMAN ACTIVITY(9,1)|COMPLEX FLOW(8,1)|GARBAGE ACCUMULATION EMBARRASSMENT(8,1)|GLOBAL CLIMATE CHANGE SOURCE(8,1)|SEMICOKE TYPE CARBON(8,1)|UNDERGROUND WATER(8,1)|BARREN FARMLAND(7,2)|URBAN DOMESTIC(7,2)|NITROGEN FERTILIZER(6,7)|PARTICLE SIZE(6,5)|CARBONIZATION TIME(6,4)|CROP POTATO(6,2)|YELLOW RIB MUD(6,2)|DAILY DOMESTIC GARBAGE(6,1)|GARBAGE PILE MIDDLE(6,1)|SOLID WASTE(6,1)|CROP YIELD(5,4)|GLOBAL CLIMATE CHANGE(5,2)|CARBONIZED DOMESTIC GARBAGE PRODUCT(5,1)|FARMER FARMLAND(5,1)|REST DOMESTIC GARBAGE(5,1)|UNBALANCED FERTILIZER(5,1)|URBANIZATION ACCELERATION(5,1)|ABSORBING SEWAGE(4,1)|BURNED SOIL(4,1)|CARBONIZATION FURNACE(4,1)|CARBONIZED PRODUCT COAPPLICATION(4,1)|GARBAGE POOL(4,1)|HOT MELTING CELLAR(4,1)|HOUSEHOLD GARBAGE CARBON CONTENT(4,1)|INCOMPLETE CARBONIZATION(4,1)|LONG CARBONIZATION TIME(4,1)|POULTRY EXCREMENT(4,1)|POULTRY MANURE(4,1)|RECOVERING WASTE IRON(4,1)|REDUCING METHANEDIONE EMISSION(4,1)|REINFORCED CURING SLURRY(4,1)|RETURNING ORGANIC GARBAGE(4,1)|SCIENTIFIC RECYCLING(4,1)|SURFACE RUNOFF(4,1)|TOOTH CHOPPER(4,1)|STRAW(3,2)|TREATING GARBAGE(3,2)|AGRICULTURAL BENEFIT(3,1)|ANIMAL BONE(3,1)|BIOCHAR CARBON CONTENT(3,1)|CARBONIZATION TREATMENT(3,1)|DUST GARBAGE(3,1)|EXTENSIVE TREATMENT(3,1)|T HM2THE FERTILIZER(3,1)|URBAN ECONOMIC CONSTRUCTION DEVELOPMENT(3,1)|VEGETABLE LEAVE(3,1)|CURING BLOCK(2,2)|FERTILITY(2,2)|LIVESTOCK(2,2)|5T HM2THE(2,1)|AUTOMATIC IRON RECOVERY MACHINE(2,1)|CARBONIZATION CONDITION(2,1)|ECONOMIC BENEFIT(2,1)|QUALITY DEGRADATION(2,1)|QUZHOU REGION(2,1)|SIGNIFICANCE(2,1)|SOIL IMPROVEMENT DEGRADATION(2,1)| (CN102583313)|1. A method for carbonizing rural domestic garbage is characterized by comprising the following steps:|(1) sorting the rural domestic garbage, and removing inorganic garbage and organic garbage which can generate toxic and harmful substances after incineration;|(2) naturally drying the sorted garbage, and then coarsely crushing to ensure that the particle size is less than or equal to 5 cm;|(3) carbonizing the coarsely crushed household garbage under an anoxic condition, wherein the carbonization temperature is 350-500 ℃, the carbonization duration is 20 min-5 h, and naturally cooling to obtain a carbonized product;|the components of the carbonized product are a mixture of biochar and burned soil.|2. A carbonized product prepared by the method for carbonizing rural domestic garbage according to claim 1.|3. The use of a charred product according to claim 2, wherein the charred product is broadcast into soil to a depth of 0-20 cm, and the charred product is applied alone or in combination with a fertilizer.|4. Use of a carbonized product according to claim 3 in which the carbonized product is applied separately in an amount of 5 to 100t/hm2。|5. The use of a carbonized product according to claim 3, wherein the carbonized product is applied in combination with a fertilizer in an amount of 5 to 100t/hm2The application amount of the fertilizer is 150-250 kg/hm2。|6. Use of a carbonized product as claimed in claim 3 or 5, characterized in that the fertilizer is a nitrogen fertilizer or a compound fertilizer. (CN102583313)|TECHNICAL FIELD|[0002] The invention relates to the technical field of rural solid waste recycling, in particular to a method for carbonizing rural domestic garbage, a product and application thereof.|BACKGROUND ART|[0004] The treatment of domestic garbage is a global problem, the garbage is accumulated in large quantity and directly pollutes soil, surface runoff, underground water and the like in a treatment mode mainly by landfill at the present stage, harmful substances, greenhouse gases such as methane and the like are released, and the human health and the environment are greatly threatened. With the continuous development of urban economic construction in China and the continuous improvement of the living standard of people, the problem is increasingly obvious and urgent, and the phenomenon of enclosing the city with garbage in many cities in inland can be proved. Meanwhile, along with the acceleration of the urbanization process of China and the reduction of farmlands of farmers, the treatment problem of rural domestic garbage is more and more serious day by day, and the research and development of the method for recycling and applying the rural domestic garbage for avoiding the embarrassment of garbage accumulation in rural areas has great practical significance.|[0005] In rural areas in Zhejiang province, the land is fertilized after carbonization by smoldering the domestic garbage, agricultural production waste and other soil methods. The traditional method is simple in operation, firstly, daily domestic garbage (mainly comprising animal and plant wastes, grass roots, fruit peels, livestock and poultry excrement and the like, which are decomposed to different degrees due to different stacking environment differences and different time lengths) is stored in a garbage pool, then the garbage is dried in the sun and piled, a plurality of straws are placed in the middle of the garbage pile, the straws are ignited, the outside of the garbage pile is covered with soil to reduce the contact between the garbage and air, the garbage pile is in a 'smoldering' state until the garbage is black, and the garbage pile is directly applied to farmlands as fertilizer after being cooled, so that the crop yield can be effectively improved. The carbonized domestic garbage product is called "Biochar" (Biochar), and the Biochar is a hot spot of current scientific research. However, in recent decades, this traditional fertilizer has been replaced by fertilisers. The massive application of fertilizers in farmlands and unreasonable agricultural production modes are main sources of non-point source pollution; unbalanced fertilizer application also induces farm quality degradation, which is disproportionate to heavy input and output.|[0006] Exacerbation of global climate change is a major political, scientific and economic problem facing people today. The increase of carbon dioxide concentration in the atmosphere caused by human activities is the most important source of global climate change, and emission reduction and carbon sequestration have become hot problems related to scientific research and international political, economic and outwork disputes. Scientific research shows that the biochar has strong stability, and has great potential for reducing carbon dioxide emission and slowing down climate change by fixing carbon by the biochar; in addition, the biochar has unusual performances in the aspects of environmental pollution treatment, degraded soil improvement, crop yield improvement and the like.|[0007] Therefore, the method for returning organic garbage to fields in Zhejiang through smoldering can be used for garbage treatment and returning to fields after carbonization, and has the function of carbon sequestration. However, the traditional method is too extensive and has the following defects: the carbonization condition is basically uncontrollable, and the problems of incomplete carbonization and excessive carbonization exist; the quantity and quality of carbonized products are not guaranteed; the domestic garbage is lack of pretreatment before carbonization, more or less inorganic substances and harmful substances exist, and the carbonized domestic garbage has potential threat to the environment.|[0008] The patent specification CN1057974A discloses a comprehensive treatment method for solid, liquid, gas and dust garbage, which comprises crushing solid garbage by a V-shaped longitudinal tooth chopper, recovering waste iron by an automatic iron recovery machine, melting and shrinking the garbage by a hot melting cellar to eliminate dust and odor, absorbing sewage and sludge from the garbage or dust, adding various curing materials, mixing into a mud-like material, pouring into a casting mold made in advance, curing, and finally adding a layer of special reinforced curing slurry outside the curing block, wherein the curing block can be used as engineering building material after drying. The method has the advantages of complex flow, more required machine equipment and higher cost.|[0009] Chinese patent No. CN1299981C discloses a process for preparing charcoal from urban and rural domestic garbage, which comprises sorting, crushing, compression molding and carbonizing the urban and rural domestic garbage to obtain semi-coke charcoal. The method aims at obtaining the semi-coke type carbon, and has the advantages of complex steps and longer carbonization time.|DISCLOSURE|[0010] Disclosure of Invention|[0011] The method for carbonizing the rural domestic garbage is economical, effective, environment-friendly, simple to operate and easy to popularize.|[0012] A method for carbonizing rural domestic garbage comprises the following steps:|[0013] (1) sorting the household garbage, and removing inorganic garbage such as waste batteries, glass, ceramics, metals and the like and organic garbage which can generate toxic and harmful substances after burning plastic products and the like;|[0014] (2) naturally drying the sorted garbage in the air, and then coarsely crushing the garbage to ensure that the particle size is less than or equal to 5 cm;|[0015] (3) carbonizing the coarsely crushed household garbage under an anoxic condition, wherein the carbonization temperature is 350-500 ℃, the carbonization time is 20 min-5 h, and naturally cooling to obtain a carbonized product.|[0016] The sorted domestic garbage mainly comprises animal and plant wastes, kitchen wastes, livestock and poultry manure, dust, soil and the like; the components of the carbonized product are a mixture of the biochar and the burned soil, and proper carbonization temperature and carbonization time are selected according to different materials and decomposition degrees thereof during carbonization.|[0017] The invention also provides a carbonized product prepared by the method.|[0018] Further, the invention also provides application of the carbonized product, the carbonized product is scattered in soil, the depth of the carbonized product applied in the soil is 0-20 cm, and the carbonized product is applied independently or matched with a fertilizer.|[0019] When the carbonized product is applied independently, the application amount is 5-100 t/hm2。|[0020] When the carbonized product is applied in combination with the fertilizer, the application amount of the carbonized product is 5-100 t/hm2The fertilizer application amount is 150-250 kg/hm2。|[0021] The fertilizer is a nitrogen fertilizer or a compound fertilizer.|[0022] The method of the invention is a scientific recycling method aiming at the condition that most of rural domestic garbage is a mixture of green organic matters and soil, and the method integrates garbage treatment, carbon fixation and recycling; the method is simple and convenient, is easy to operate and popularize, has wide application range of the carbonized product, does not generate secondary pollution, and has obvious agricultural benefit, economic benefit and environmental benefit.|INVENTION MODE|[0023] Detailed Description|[0024] Example 1 carbonization treatment of rural domestic garbage|[0025] Collecting domestic garbage in Zhejiang rural areas, sorting the domestic garbage, and removing inorganic garbage such as metal, glass, ceramic and the like and organic garbage which can generate toxic and harmful substances after burning waste plastics and the like, wherein the rest domestic garbage mainly comprises fruit peels, vegetable leaves, grass roots, animal bones, soil, dust and the like; naturally drying the sorted domestic garbage (the water content is less than or equal to 10 percent), and roughly crushing to ensure that the particle size is less than or equal to 5 cm; and (3) putting the coarsely crushed household garbage into a carbonization furnace for carbonization under the anoxic condition, wherein the carbonization temperature is 430 ℃, the carbonization time is 40min, and naturally cooling to obtain a black coke-shaped carbonized product. The carbon content of the household garbage 1t before carbonization is 300-600 kg, the carbon content of the biochar in the obtained carbonized product is 150-300 kg, and the carbon fixing rate is about 50%.|[0026] Example 2 application of carbonized products of rural domestic garbage in barren farmland|[0027] Selecting a 'yellow rib mud' type farmland which is universally distributed in Jinhua and Quzhou areas of Zhejiang, wherein the surface soil of the test field is shallow, the fertility is low, the test field belongs to a low-yield field, the area is 0.2 mu, crushing about 200kg of the carbonized product prepared in the embodiment 1 of the invention to the particle size of less than or equal to 2mm, spreading the carbonized product on the soil surface of the test field, and the application amount of the carbonized product is about 15t/hm2And ploughing the soil to a depth of about 20cm, and selecting a farmland which is close to the test field and is not applied with the carbonized product and has the same area as the control field.Local common crop potatoes are taken as test objects. During the first growth period, the potatoes grew better in the test field with the carbonized product compared to the control field without the carbonized product, and the yield of the potatoes was 9.6t/hm2On the other hand, some potatoes in the control field can not even complete the growth period, and the yield of the potatoes is about 7.5t/hm2The application of the carbonized product of the invention has good improvement effect on soil and improves the yield of crops.|[0028] Example 3 application of carbonized product of rural domestic garbage and fertilizer in barren farmland|[0029] A 'yellow rib mud' type farmland which is universally distributed in Jinhua and Quzhou regions of Zhejiang is selected to be provided with a test field, the surface soil of the test field is shallow, the fertility is low, the test field belongs to a low-yield field, and the area is 0.2 mu. The carbonized product prepared in the embodiment 1 of the invention is crushed to the grain diameter of less than or equal to 2mm by about 200kg, and is spread on the soil surface of the test field, and the application amount is about 15t/hm2At the same time, 150kg/hm of nitrogen fertilizer is applied2And ploughing the soil to a depth of about 20 cm. Selecting a farmland with the same ground condition and the same area close to the test field as a control field, wherein the control field is not applied with the carbonized product, and the other treatment modes are consistent with those of the test field simultaneously applied with the carbonized product and the nitrogen fertilizer. Common crop potatoes are used as test objects. In the first growth period, the yield of the potatoes in the test field where the nitrogen fertilizer and the carbonized product are cooperatively applied is about 12.5t/hm2While the potato yield of the control field with nitrogen fertilizer alone was about 8.3t/hm2. The field test shows that the yield of the potatoes can be obviously increased by the co-application of the carbonized product and the nitrogen fertilizer. (CN102583313)|TECHNICAL FIELD|[0002] The invention relates to the technical field of rural solid waste recycling, in particular to a method for carbonizing rural domestic garbage, a product and application thereof.|BACKGROUND ART|[0004] The treatment of domestic garbage is a global problem, the garbage is accumulated in large quantity and directly pollutes soil, surface runoff, underground water and the like in a treatment mode mainly by landfill at the present stage, harmful substances, greenhouse gases such as methane and the like are released, and the human health and the environment are greatly threatened. With the continuous development of urban economic construction in China and the continuous improvement of the living standard of people, the problem is increasingly obvious and urgent, and the phenomenon of enclosing the city with garbage in many cities in inland can be proved. Meanwhile, along with the acceleration of the urbanization process of China and the reduction of farmlands of farmers, the treatment problem of rural domestic garbage is more and more serious day by day, and the research and development of the method for recycling and applying the rural domestic garbage for avoiding the embarrassment of garbage accumulation in rural areas has great practical significance.|[0005] In rural areas in Zhejiang province, the land is fertilized after carbonization by smoldering the domestic garbage, agricultural production waste and other soil methods. The traditional method is simple in operation, firstly, daily domestic garbage (mainly comprising animal and plant wastes, grass roots, fruit peels, livestock and poultry excrement and the like, which are decomposed to different degrees due to different stacking environment differences and different time lengths) is stored in a garbage pool, then the garbage is dried in the sun and piled, a plurality of straws are placed in the middle of the garbage pile, the straws are ignited, the outside of the garbage pile is covered with soil to reduce the contact between the garbage and air, the garbage pile is in a 'smoldering' state until the garbage is black, and the garbage pile is directly applied to farmlands as fertilizer after being cooled, so that the crop yield can be effectively improved. The carbonized domestic garbage product is called "Biochar" (Biochar), and the Biochar is a hot spot of current scientific research. However, in recent decades, this traditional fertilizer has been replaced by fertilisers. The massive application of fertilizers in farmlands and unreasonable agricultural production modes are main sources of non-point source pollution; unbalanced fertilizer application also induces farm quality degradation, which is disproportionate to heavy input and output.|[0006] Exacerbation of global climate change is a major political, scientific and economic problem facing people today. The increase of carbon dioxide concentration in the atmosphere caused by human activities is the most important source of global climate change, and emission reduction and carbon sequestration have become hot problems related to scientific research and international political, economic and outwork disputes. Scientific research shows that the biochar has strong stability, and has great potential for reducing carbon dioxide emission and slowing down climate change by fixing carbon by the biochar; in addition, the biochar has unusual performances in the aspects of environmental pollution treatment, degraded soil improvement, crop yield improvement and the like.|[0007] Therefore, the method for returning organic garbage to fields in Zhejiang through smoldering can be used for garbage treatment and returning to fields after carbonization, and has the function of carbon sequestration. However, the traditional method is too extensive and has the following defects: the carbonization condition is basically uncontrollable, and the problems of incomplete carbonization and excessive carbonization exist; the quantity and quality of carbonized products are not guaranteed; the domestic garbage is lack of pretreatment before carbonization, more or less inorganic substances and harmful substances exist, and the carbonized domestic garbage has potential threat to the environment.|[0008] The patent specification CN1057974A discloses a comprehensive treatment method for solid, liquid, gas and dust garbage, which comprises crushing solid garbage by a V-shaped longitudinal tooth chopper, recovering waste iron by an automatic iron recovery machine, melting and shrinking the garbage by a hot melting cellar to eliminate dust and odor, absorbing sewage and sludge from the garbage or dust, adding various curing materials, mixing into a mud-like material, pouring into a casting mold made in advance, curing, and finally adding a layer of special reinforced curing slurry outside the curing block, wherein the curing block can be used as engineering building material after drying. The method has the advantages of complex flow, more required machine equipment and higher cost.|[0009] Chinese patent No. CN1299981C discloses a process for preparing charcoal from urban and rural domestic garbage, which comprises sorting, crushing, compression molding and carbonizing the urban and rural domestic garbage to obtain semi-coke charcoal. The method aims at obtaining the semi-coke type carbon, and has the advantages of complex steps and longer carbonization time.|DISCLOSURE|[0010] Disclosure of Invention|[0011] The method for carbonizing the rural domestic garbage is economical, effective, environment-friendly, simple to operate and easy to popularize.|[0012] A method for carbonizing rural domestic garbage comprises the following steps:|[0013] (1) sorting the household garbage, and removing inorganic garbage such as waste batteries, glass, ceramics, metals and the like and organic garbage which can generate toxic and harmful substances after burning plastic products and the like;|[0014] (2) naturally drying the sorted garbage in the air, and then coarsely crushing the garbage to ensure that the particle size is less than or equal to 5 cm;|[0015] (3) carbonizing the coarsely crushed household garbage under an anoxic condition, wherein the carbonization temperature is 350-500 ℃, the carbonization time is 20 min-5 h, and naturally cooling to obtain a carbonized product.|[0016] The sorted domestic garbage mainly comprises animal and plant wastes, kitchen wastes, livestock and poultry manure, dust, soil and the like; the components of the carbonized product are a mixture of the biochar and the burned soil, and proper carbonization temperature and carbonization time are selected according to different materials and decomposition degrees thereof during carbonization.|[0017] The invention also provides a carbonized product prepared by the method.|[0018] Further, the invention also provides application of the carbonized product, the carbonized product is scattered in soil, the depth of the carbonized product applied in the soil is 0-20 cm, and the carbonized product is applied independently or matched with a fertilizer.|[0019] When the carbonized product is applied independently, the application amount is 5-100 t/hm2。|[0020] When the carbonized product is applied in combination with the fertilizer, the application amount of the carbonized product is 5-100 t/hm2The fertilizer application amount is 150-250 kg/hm2。|[0021] The fertilizer is a nitrogen fertilizer or a compound fertilizer.|[0022] The method of the invention is a scientific recycling method aiming at the condition that most of rural domestic garbage is a mixture of green organic matters and soil, and the method integrates garbage treatment, carbon fixation and recycling; the method is simple and convenient, is easy to operate and popularize, has wide application range of the carbonized product, does not generate secondary pollution, and has obvious agricultural benefit, economic benefit and environmental benefit.|INVENTION MODE|[0023] Detailed Description|[0024] Example 1 carbonization treatment of rural domestic garbage|[0025] Collecting domestic garbage in Zhejiang rural areas, sorting the domestic garbage, and removing inorganic garbage such as metal, glass, ceramic and the like and organic garbage which can generate toxic and harmful substances after burning waste plastics and the like, wherein the rest domestic garbage mainly comprises fruit peels, vegetable leaves, grass roots, animal bones, soil, dust and the like; naturally drying the sorted domestic garbage (the water content is less than or equal to 10 percent), and roughly crushing to ensure that the particle size is less than or equal to 5 cm; and (3) putting the coarsely crushed household garbage into a carbonization furnace for carbonization under the anoxic condition, wherein the carbonization temperature is 430 ℃, the carbonization time is 40min, and naturally cooling to obtain a black coke-shaped carbonized product. The carbon content of the household garbage 1t before carbonization is 300-600 kg, the carbon content of the biochar in the obtained carbonized product is 150-300 kg, and the carbon fixing rate is about 50%.|[0026] Example 2 application of carbonized products of rural domestic garbage in barren farmland|[0027] Selecting a 'yellow rib mud' type farmland which is universally distributed in Jinhua and Quzhou areas of Zhejiang, wherein the surface soil of the test field is shallow, the fertility is low, the test field belongs to a low-yield field, the area is 0.2 mu, crushing about 200kg of the carbonized product prepared in the embodiment 1 of the invention to the particle size of less than or equal to 2mm, spreading the carbonized product on the soil surface of the test field, and the application amount of the carbonized product is about 15t/hm2And ploughing the soil to a depth of about 20cm, and selecting a farmland which is close to the test field and is not applied with the carbonized product and has the same area as the control field.Local common crop potatoes are taken as test objects. During the first growth period, the potatoes grew better in the test field with the carbonized product compared to the control field without the carbonized product, and the yield of the potatoes was 9.6t/hm2On the other hand, some potatoes in the control field can not even complete the growth period, and the yield of the potatoes is about 7.5t/hm2The application of the carbonized product of the invention has good improvement effect on soil and improves the yield of crops.|[0028] Example 3 application of carbonized product of rural domestic garbage and fertilizer in barren farmland|[0029] A 'yellow rib mud' type farmland which is universally distributed in Jinhua and Quzhou regions of Zhejiang is selected to be provided with a test field, the surface soil of the test field is shallow, the fertility is low, the test field belongs to a low-yield field, and the area is 0.2 mu. The carbonized product prepared in the embodiment 1 of the invention is crushed to the grain diameter of less than or equal to 2mm by about 200kg, and is spread on the soil surface of the test field, and the application amount is about 15t/hm2At the same time, 150kg/hm of nitrogen fertilizer is applied2And ploughing the soil to a depth of about 20 cm. Selecting a farmland with the same ground condition and the same area close to the test field as a control field, wherein the control field is not applied with the carbonized product, and the other treatment modes are consistent with those of the test field simultaneously applied with the carbonized product and the nitrogen fertilizer. Common crop potatoes are used as test objects. In the first growth period, the yield of the potatoes in the test field where the nitrogen fertilizer and the carbonized product are cooperatively applied is about 12.5t/hm2While the potato yield of the control field with nitrogen fertilizer alone was about 8.3t/hm2. The field test shows that the yield of the potatoes can be obviously increased by the co-application of the carbonized product and the nitrogen fertilizer. Family Number|(7788454)|7788454|Abstract|(CN102583313B B)|The invention discloses a rural household garbage carbonization method , prepared products using same , and an application . The method comprises steps of sorting household garbage , rejecting inorganic garbage and organic garbage capable of generating toxic hazardous substance through burning , performing natural air drying on the sorted garbage , performing coarse crushing on the sorted garbage to enable the particle diameter of the garbage to be no more than 5 cm , subjecting the garbage after being crushed coarsely to carbonization for a time from 20 minutes to 5 hours at a temperature in a range between 350 DEG C and 500 DEG C under the condition of oxygen deficiency , cooling naturally the garbage , and obtaining the carbonization products . The rural household garbage carbonization method , the prepared products using the same , and the application combine rural household garbage processing , resource application and carbon sequestration and have the advantages of being economic , effective , environment - friendly , easy in operation , and easy to popularize . As fertilizers , the prepared carbonization products improve farmland soil and crop output and cannot generate secondary pollution . |IPC codes|(CN102583313B B)|A01C - 021/00 |C01B - 032/05 | Basic materials chemistry|Materials, metallurgy|Other special machines Y02A-040/20 Y02A-040/20 A01C-021/00|C01B-032/05|C05F-009/00|C05G-001/00 A01C-021/00|C01B-031/02|C05F-009/00|C05G-001/00 CN106518505|CN104058899|CN104261950|CN109621900|CN109621901|CN106122968|CN104557160B|CN103449925B|CN103450907B|CN103265962B CN106518505 75703954 WHO=Examiner SELF=N CAT=Y|CN104058899 67504807 WHO=Examiner SELF=N CAT=Y|CN104261950 68331642 WHO=Examiner SELF=N CAT=X|CN109621900 84174403 WHO=Examiner SELF=N CAT=A|CN109621901 84181103 WHO=Examiner SELF=N CAT=A|CN106122968 74602264 WHO=Examiner SELF=N CAT=A|CN104557160B 69239555 WHO=Examiner SELF=N|CN103449925B 59440855 WHO=Examiner SELF=N|CN103450907B 59443588 WHO=Examiner SELF=Y|CN103265962B 45870340 WHO=Examiner SELF=Y CN101397503|CN1644492|CN1361058|CN1235072 CN101397503 62164335 WHO=Examiner SELF=N|CN1644492 5001850 WHO=Examiner SELF=N|CN1361058 4928371 WHO=Examiner SELF=N|CN1235072 4977734 WHO=Examiner SELF=N CN 1644492 A,2005.07.27,说明书第3页第1-13行.|CN 1235072 A,1999.11.17,说明书摘要,权利要求1-6.|CN 101397503 A,2009.04.01,说明书实施例1-4.|CN 1361058 A,2002.07.31,说明书实施例1-3. CN1644492; CN1235072; CN101397503; CN1361058 LAPSED (CN102583313)|LAPSED DEAD (CN102583313)|DEAD (CN102583313)|LEGAL DETAILS FOR CN102583313|Actual or expected expiration date=2018-02-14|Legal state=DEAD|Status=LAPSED|Event publication date=2012-02-14|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201210032120|Application date=2012-02-14|Standardized application number=2012CN-0032120|Event publication date=2012-07-18|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN102583313|Publication stage code=A|Publication date=2012-07-18|Standardized publication number=CN102583313|Event publication date=2012-07-18|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2012-09-19|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2013-10-23|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN102583313|Publication stage code=B|Publication date=2013-10-23|Standardized publication number=CN102583313B|Event publication date=2013-10-23|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2019-02-01|Event code=CN/CF01|Event indicator=Neg|Event group=Event indicating Not In Force|Termination of patent right due to non-payment of annual fee|Effective date of the event=2018-02-14 https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjnR0xWMDm65dRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252FqRpO%252BXYFx9dGLM0zuZb6LmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN102583313)|NAME=HU HONGJUAN;HANGZHOU TIANQIN INTELLECTUAL PROPERTY AGENCY CO LTD|(CN102583313)|NAME=HU HONGJUAN;HANGZHOU TIANQIN INTELLECTUAL PROPERTY AGENCY CO LTD (CN102583313)|NAME=WU JIAPING|NAME=ZHAO RUDONG|(CN102583313)|NAME=WU JIAPING|NAME=ZHAO RUDONG 0 1 Titre: (CN102583313)|Rural household garbage carbonization method, prepared products using same, and application Résumé: (CN102583313)|The invention discloses a rural household garbage carbonization method, prepared products using same, and an application. The method comprises steps of sorting household garbage, rejecting inorganic garbage and organic garbage capable of generating toxic hazardous substance through burning, performing natural air drying on the sorted garbage, performing coarse crushing on the sorted garbage to enable the particle diameter of the garbage to be no more than 5 cm, subjecting the garbage after being crushed coarsely to carbonization for a time from 20 minutes to 5 hours at a temperature in a range between 350 DEG C and 500 DEG C under the condition of oxygen deficiency, cooling naturally the garbage, and obtaining the carbonization products. The rural household garbage carbonization method, the prepared products using the same, and the application combine rural household garbage processing, resource application and carbon sequestration and have the advantages of being economic, effective,environment-friendly, easy in operation, and easy to popularize. As fertilizers, the prepared carbonization products improve farmland soil and crop output and cannot generate secondary pollution. 80 Abstract gpt-4o-mini no The article focuses on a carbonization method for household garbage and its applications, which does not involve accelerated weathering of minerals or CO₂ capture through mineral carbonation.
81 JP2009019549 JP2009019549 JP2010173909 33171765 JP2010173909 A 2010-08-12 [JP2010173909] 2009-01-30 2009-01-30 2010-08-12 (JP2010173909)|2019-08-12 (JP2010173909)|Carbon dioxide removal device (JP2010173909)|PROBLEM TO BE SOLVED: To provide a device which suppresses discharge of carbon dioxide which is considered to be one of the causes of global warming.SOLUTION: The device for removing or reducing carbon dioxide comprises mixing a powders 1 burned and crushed seashells with water and catalyst, passing exhaust gas 3 including carbon dioxide which is discharged at the time of burning in the solution, and causing chemical change or chemical reaction. The seashells piled outdoor as a waste material are incinerated, powdered, and are made to cause the chemical reaction, so as to be able to produce harmless calcium dioxide. The device is excellent from the viewpoint of the treatment of waste.COPYRIGHT: (C)2010,JPO&INPIT MIYACHI YOSHINOBU (JP2010173909)|MIYACHI YOSHINOBU MIYACHI YOSHINOBU (JP2010173909)|MIYACHI YOSHINOBU (JP2010173909)|1. A device for removing carbon dioxide by mixing a powder obtained by burning and pulverizing a shell with water and a catalyst and allowing a gas containing carbon dioxide to pass through the solution, thereby causing chemical changes and removing carbon dioxide.| (JP2010173909)|[Problem] To provide a device that suppresses the emission of carbon dioxide as one cause of global warming. Resolution Means: a device for removing and reducing carbon dioxide by mixing a powder 1 obtained by burning and pulverizing a shell with water and a catalyst, and passing exhaust gas 3 containing carbon dioxide discharged during combustion through the solution to cause chemical changes and reactions.| (JP2010173909)|CARBON DIOXIDE(100,11)|SHELL(100,4)|GAS(100,3)|CATALYST(100,2)|CHEMICAL CHANGE(100,2)|POWDER(100,2)|CARBON DIOXIDE REMOVAL(100,1)|CARBON DIOXIDE EMISSION(88,1)|GLOBAL WARMING(77,1)|HARMLESS CALCIUM DIOXIDE(74,1)|COMBUSTION(71,1)|FIRE(42,1)|EXHAUST GAS(40,1)|WASTE TREATMENT(28,1)| (JP2010173909)|1. A device for removing carbon dioxide by mixing a powder obtained by burning and pulverizing a shell with water and a catalyst and allowing a gas containing carbon dioxide to pass through the solution, thereby causing chemical changes and removing carbon dioxide. (JP2010173909)|CITATION LIST|NON PATENT LITERATURE|[0001] Non-Patent Document n|DESCRIPTION OF DRAWINGS|[0002] This is an explanatory diagram illustrating a method for removing carbon dioxide.|REFERENCE SIGNS LIST|[0003] 1 Aqueous solution of powder obtained by burning and pulverizing a shell, 2 Aqueous solution obtained by chemical reaction with carbon dioxide, 3 Gas containing carbon dioxide, 4 Gas after carbon dioxide treatment, 5 during chemical reaction in bubble form (JP2010173909)|CITATION LIST|NON PATENT LITERATURE|[0001] Non-Patent Document n|DESCRIPTION OF DRAWINGS|[0002] This is an explanatory diagram illustrating a method for removing carbon dioxide.|REFERENCE SIGNS LIST|[0003] 1 Aqueous solution of powder obtained by burning and pulverizing a shell, 2 Aqueous solution obtained by chemical reaction with carbon dioxide, 3 Gas containing carbon dioxide, 4 Gas after carbon dioxide treatment, 5 during chemical reaction in bubble form Family Number|(33171765)|33171765|Abstract|(JP2010173909 A)|PROBLEM TO BE SOLVED: To provide a device which suppresses discharge of carbon dioxide which is considered to be one of the causes of global warming.SOLUTION: The device for removing or reducing carbon dioxide comprises mixing a powders 1 burned and crushed seashells with water and catalyst, passing exhaust gas 3 including carbon dioxide which is discharged at the time of burning in the solution, and causing chemical change or chemical reaction. The seashells piled outdoor as a waste material are incinerated, powdered, and are made to cause the chemical reaction, so as to be able to produce harmless calcium dioxide. The device is excellent from the viewpoint of the treatment of waste.COPYRIGHT: (C)2010,JPO&INPIT|IPC codes|(JP2010173909 A)|C01B-031/20|C01B-032/50|Title|(JP2010173909 A)|Carbon dioxide removal device| Materials, metallurgy C01B-031/20|C01B-032/50 C01B-031/20 LAPSED (JP2010173909)|LAPSED DEAD (JP2010173909)|DEAD (JP2010173909)|LEGAL DETAILS FOR JP2010173909|Actual or expected expiration date=2019-08-12|Legal state=DEAD|Status=LAPSED|Event publication date=2009-01-30|Event code=JP/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=JP JP2009019549|Application date=2009-01-30|Standardized application number=2009JP-0019549|Event publication date=2010-08-12|Event code=JP/A|Event group=Examination events|Published application|Publication country=JP|Publication number=JP2010173909|Publication stage code=A|Publication date=2010-08-12|Standardized publication number=JP2010173909|Event publication date=2019-08-12|Event code=JP/EEDL|Event indicator=Neg|Event group=Event indicating Not In Force|Pending application likely abandoned https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=N5221X+da3+7j3PhffOi+QMqfaYWomYVbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=JP2010173909&ekey=1539&xpn=JP2010173909&kind=A https://www.j-platpat.inpit.go.jp/c1801/PU/JP-2009-019549/10/en https://permalink.orbit.com/RenderStaticFirstPage?XPN=U7XPC2Zvw5R30XI450KTLLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT JP (JP2010173909)|NAME=MIYACHI YOSHINOBU 0 1 Titre: (JP2010173909)|Carbon dioxide removal device Résumé: (JP2010173909)|PROBLEM TO BE SOLVED: To provide a device which suppresses discharge of carbon dioxide which is considered to be one of the causes of global warming.SOLUTION: The device for removing or reducing carbon dioxide comprises mixing a powders 1 burned and crushed seashells with water and catalyst, passing exhaust gas 3 including carbon dioxide which is discharged at the time of burning in the solution, and causing chemical change or chemical reaction. The seashells piled outdoor as a waste material are incinerated, powdered, and are made to cause the chemical reaction, so as to be able to produce harmless calcium dioxide. The device is excellent from the viewpoint of the treatment of waste.COPYRIGHT: (C)2010,JPO&INPIT 81 Abstract gpt-4o-mini no The patent focuses on a device for removing carbon dioxide from exhaust gases using incinerated seashells, which does not involve accelerated weathering of silicate or alkaline minerals for carbon sequestration.
82 CN202411750392 CN202411750392 CN119706889 113961434 CN119706889 A 2025-03-28 [CN119706889] 2024-12-02 2024-12-02 2025-03-28 (CN119706889)|2044-12-02 (CN119706889)|Method for preparing battery-grade lithium carbonate from electrolytic aluminum waste (CN119706889)|The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for preparing battery-grade lithium carbonate from electrolytic aluminum waste. The method comprises the following steps: (1) coarsely crushing the electrolytic aluminum waste; (2) calcining or combusting the coarsely crushed material to remove carbon, then performing fine grinding, and adsorbing magnetic substances by using a demagnetizer; (3) leaching: carrying out two-stage leaching on the material subjected to carbon removal; (4) impurity removal: performing two-stage impurity removal on the first-stage leachate; and (5) carrying out concentration, denitration, lithium precipitation and refining on the lithium solution after impurity removal to prepare the battery-grade lithium carbonate. The electrolytic aluminum waste residues are firstly subjected to carbon removal, the lithium extraction treatment capacity and the leaching rate are improved, ferromagnetic substances in the raw materials are removed through a magnetic removal method, the use amount of leaching acid and the use amount of impurity removal oxidizing agents and alkali are reduced, the main component of impurity removal residues is aluminum hydroxide with high purity and can be directly utilized, the treatment difficulty and cost are greatly reduced, and the method is suitable for industrial production. The lithium recovery rate and the treatment efficiency are improved. JINCHUAN|LANZHOU JINCHUAN SCIENCE PARK (CN119706889)|JINCHUAN GROUP CO. LTD. ([CN])|LANZHOU JINCHUAN SCIENCE PARK CO LTD CHAI GENFENG|HU JIAYAN|YANG XIAOYAN|WANG JUANHUI|XIE YI|HUO WENSHENG|HUANG SHUWEN|HE YAN|ZHANG JIALE|MA JIANJI|TANG PENGJUN (CN119706889)|CHAI GENFENG|HU JIAYAN|YANG XIAOYAN|WANG JUANHUI|XIE YI|HUO WENSHENG|HUANG SHUWEN|HE YAN|ZHANG JIALE|MA JIANJI|TANG PENGJUN (CN119706889)|LI ZIJIAN;CHINA NONFERROUS METALS INDUSTRY PATENT CENTER|Reg. Nb: 11028 (CN119706889)|(3) The invention adopts two sections of normal pressure leaching, improves the leaching rate of lithium as much as possible by controlling the leaching conditions, and has the advantages of leaching condition mildness, no high temperature and high pressure condition, high safety coefficient, low treatment cost and easy operation, and the leaching rate of lithium can reach more than 99 percent.|Compared with the prior art, the invention has the following advantages:|The method uses sulfating roasting process-water leaching precipitation-causticization-lithium precipitation to prepare battery grade lithium carbonate, and has the advantages of long flow, high reagent consumption, high energy consumption and large pollution.|(4) In addition, oxalic acid is used as a decalcifying agent instead of conventional ion exchange resin in the two-stage impurity removal process, so that excessive waste water can be avoided, the problem that the ion exchange resin is easy to scale in a sulfuric acid system is avoided, and the high-efficiency decalcifying and smooth system operation can be realized.|Development of industries such as automobiles drives the growth of nonferrous metal demands, the electrolytic aluminum industry expands in batches, electrolytic aluminum waste residues contain a certain amount of lithium, and the materials are high in impurity content, particularly high in aluminum content, difficult to process and high in processing cost.| (CN119706889)|1. The method for preparing the battery grade lithium carbonate by electrolyzing the aluminum scraps is characterized by comprising the following steps of: step 1, crushing electrolytic aluminum waste with carbon content more than 50%, aluminum content 5-7 times of lithium content and iron content at least 2 times of lithium content; Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and finely grinding to obtain a decarbonized material by adsorbing magnetic substances therein by a magnetic remover; Step 3, carrying out two-stage sulfuric acid leaching on the decarbonized material, controlling the pH value of the first-stage leaching to be 1.3-1.6, filtering after the first-stage leaching to obtain a first-stage leaching solution and a first-stage leaching residue, carrying out two-stage leaching on the first-stage leaching residue, controlling the pH value of the second-stage leaching to be 0.5-1.0 to obtain a second-stage leaching solution and a second-stage leaching residue, and returning the second-stage leaching solution to the first-stage leaching process; Step 4, performing two-stage impurity removal, wherein the one-stage impurity removal process comprises the steps of adding an oxidant into the first-stage leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues; Step 5, heating and concentrating the filtrate containing lithium, and then freezing and crystallizing to obtain a denitration liquid; Step 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate; And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. | (CN119706889)|The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for preparing battery-grade lithium carbonate from electrolytic aluminum waste.| (CN119706889)|LITHIUM CARBONATE(100,51)|ALUMINUM ELECTROLYTE(100,16)|BATTERY GRADE LITHIUM CARBONATE(100,13)|BATTERY(100,8)|ALUMINUM SCRAP(100,4)|ELECTROLYTIC ALUMINUM LITHIUM(97,2)|BATTERY GRADE(88,9)|ELECTROLYTIC ALUMINUM WASTE(81,6)|SULFATING ROASTING(76,1)|LEACHING(65,24)|CRUSHED ELECTROLYTIC ALUMINUM(59,3)|MAGNETIC REMOVER(55,4)|REAGENT CONSUMPTION(51,1)|REMOVING IMPURITY(49,12)|IMPURITY REMOVAL OXIDANT(49,1)|COARSE CRUSHING(45,1)|FERROMAGNETIC SUBSTANCE(44,1)|SAFETY COEFFICIENT(44,1)|ELECTROLYTIC ALUMINUM WASTE RESIDUE(43,4)|LEACHING RESIDUE(43,1)|MAGNETIC SUBSTANCE ADSORPTION(43,1)|LITHIUM CONTENT(41,7)|CRUDE SODIUM CARBONATE(40,6)|DECALCIFICATION(40,1)|IMPURITY CONTENT(39,1)|WASTEWATER(39,1)|IMPURITY REMOVAL RESIDUE(38,1)|LEACHING CONDITION(38,1)|CRUDE LITHIUM CARBONATE(37,12)|ION EXCHANGE RESIN(37,2)|LEACHED ACID(36,1)|ALUMINUM ELECTROLYTE RESIDUE(35,6)|CONCENTRATION DENITRATION LITHIUM(35,1)|LITHIUM(34,27)|DENITRATION LIQUID(34,3)|NONFERROUS METAL DEMAND GROWTH(34,1)|ALUMINUM CONTENT(32,6)|ALUMINUM WASTE RESIDUE(32,3)|COARSE CRUSHED MATERIAL DECARBONIZATION(32,1)|STAGE LEACHING(31,10)|MILDNESS(30,1)|MAGNETIC SUBSTANCE(29,7)|FILTRATE(28,23)|DENITRATION(28,10)|LITHIUM EXTRACTION TREATMENT(28,2)|ELECTROLYTIC ALUMINUM INDUSTRY(27,2)|ADDED CALCIUM REMOVER(27,1)|NONFERROUS METAL DEMAND(27,1)|STAGE SULFURIC ACID(27,1)|STAGE IMPURITY REMOVAL(26,12)|FREEZING CRYSTALIZATION TEMPERATURE(26,2)|ELECTROLYTIC ALUMINUM SCRAP SIZE(26,1)|FILTER RESIDUE(25,18)|SODIUM CARBONATE(25,14)|ALUMINUM RESIDUE(25,6)|OXIDANT(25,3)|ION EXCHANGE(24,2)|TREATMENT DIFFICULTY(24,2)|MAGNETIC FORCE REMOVAL(24,1)|CRYSTALIZATION(23,6)|IMPURITY REMOVAL(23,4)|BATCH(23,1)|FREEZING(20,4)|LARGE POLLUTION(20,1)|CARBON CONTENT(19,5)|HEATED CONDITION(19,3)|REMOVING CARBON(19,1)|LITHIUM SOLUTION(18,7)|LITHIUM CARBONATE SOLUTION(18,6)|CALCINATION(18,5)|PROCESSING COST(18,1)|HEATING CRYSTALIZATION TEMPERATURE(17,3)|LEACHING TEMPERATURE(17,3)|STAGE LEACHING(17,3)|SULFURIC ACID(16,16)|SODIUM CARBONATE SOLUTION(16,4)|ELECTROLYTIC ALUMINUM WASTE MATERIAL(16,2)|PRIMARY LEACHING SLAG(15,4)|IMPURITY REMOVAL TEMPERATURE(15,3)|LEACHING KETTLE(15,3)|GRINDING(15,2)|DECARBONIZE MATERIAL(15,1)|PRESSURE CONDITION(15,1)|LITHIUM RECOVERY RATE(14,2)|NORMAL PRESSURE LEACHING(14,1)|OXALIC ACID(13,7)|MANGANESE(13,3)|FILTER LIQUOR(12,6)|ALUMINUM INDUSTRY(12,2)|PRIMARY LEACHING PULPING(12,2)|HEATING TEMPERATURE(11,3)|SODIUM HYDROXIDE SOLUTION(11,3)|CRUSHED ELECTROLYTIC ALUMINUM SCRAP(11,1)|FOREIGN LITHIUM RESOURCE(10,1)|LEACHED SLAG(10,1)|TREATMENT COST(10,1)|PURE WATER(9,10)|SLURRY LIQUID SOLID RATIO(9,5)|IRON LEACHING RATE(9,3)|PRECISE FILTRATION(9,3)|EXTRACTING LITHIUM(9,2)|CRUSHED ELECTROLYTIC ALUMINUM WASTE(9,1)|NORMAL PRESSURE LEACHING SECTION(9,1)|MASS FRACTION(8,3)|WASHING LIQUID(8,3)|CRUCIBLE(7,4)|DEMAGNETIZER(7,4)|REMOVING CALCIUM(7,4)|MASS CONCENTRATION(7,3)|DENITRATED LIQUID(7,2)|LONG FLOW(7,2)|COMPANY LAYOUT(7,1)|IMPURITY FILTERING RESIDUE(7,1)|LITHIUM EXTRACTION DEVELOPMENT(7,1)|LITHIUM FULL LEACHING(7,1)|LEACHING TIME(6,4)|ABSORPTION LIQUID(6,3)|CALCINER(6,3)|CALCIUM REMOVING OXALIC ACID(6,3)|DENITRATING(6,3)|DISSOLUTION(6,3)|HF GAS(6,3)|MASS RATIO(6,3)|ALUMINUM HYDROXIDE PRECIPITATE SLAG(6,1)|CAUSTICIZATION REACTION(6,1)|ECONOMIC BENEFIT(6,1)|INTRODUCING FILTRATE(6,1)|HIGH ENERGY CONSUMPTION(5,2)|PRIMARY LEACHING LIQUID(5,2)|PRIMARY LEACHING SOLUTION(5,2)|ALUMINUM PRECIPITATION(5,1)|BYPRODUCT(5,1)|CARBONIZATION REACTION(5,1)|FLUORINE CONTENT(5,1)|FREEZE CRYSTALIZATION TEMPERATURE(5,1)|REACTION KETTLE(5,1)| (CN119706889)|1. The method for preparing the battery grade lithium carbonate by electrolyzing the aluminum scraps is characterized by comprising the following steps of:| step 1, crushing electrolytic aluminum waste with carbon content more than 50%, aluminum content 5-7 times of lithium content and iron content at least 2 times of lithium content; | Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and finely grinding to obtain a decarbonized material by adsorbing magnetic substances therein by a magnetic remover; | Step 3, carrying out two-stage sulfuric acid leaching on the decarbonized material, controlling the pH value of the first-stage leaching to be 1.3-1.6, filtering after the first-stage leaching to obtain a first-stage leaching solution and a first-stage leaching residue, carrying out two-stage leaching on the first-stage leaching residue, controlling the pH value of the second-stage leaching to be 0.5-1.0 to obtain a second-stage leaching solution and a second-stage leaching residue, and returning the second-stage leaching solution to the first-stage leaching process; | Step 4, performing two-stage impurity removal, wherein the one-stage impurity removal process comprises the steps of adding an oxidant into the first-stage leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues; | Step 5, heating and concentrating the filtrate containing lithium, and then freezing and crystallizing to obtain a denitration liquid; | Step 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate; | And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. |2. The method for preparing battery grade lithium carbonate from electrolytic aluminum scraps according to claim 1, wherein the electrolytic aluminum scraps in the step 1 comprise 1% -1.2% of lithium, 5.5% -6.6% of aluminum, 9.5% -10.0% of sodium, 2.2% -2.5% of iron, 1.0% -1.3% of calcium, 0.24% -0.26% of magnesium, 2.5% -2.9% of silicon, 6.0% -6.5% of fluorine, 0.14% -0.15% of sulfur, 0.1% of manganese, 50% of carbon and the balance of water.|3. The method for preparing battery grade lithium carbonate from electrolytic aluminum scraps according to claim 1, wherein the size of the electrolytic aluminum scraps crushed in the step 1 is 1-10cm.|4. The method for preparing battery grade lithium carbonate by using electrolytic aluminum waste according to claim 1, wherein in the leaching process in the step 3, the leaching agent is sulfuric acid with the mass fraction of 98%, the leaching temperature is 60-90 ℃, the leaching time is 1-5h, the slurry liquid-solid ratio of water to decarbonized materials in the first leaching stage is 3-10:1, the slurry liquid-solid ratio of the second leaching stage is 2-5:1, and the washing liquid is returned to the first leaching stage after the second leaching residue is washed.|5. The method for preparing battery grade lithium carbonate by using electrolytic aluminum waste material according to claim 1, wherein the oxidant in the first stage of impurity removal process in the step 4 is air, the impurity removal temperature is 55-70 ℃, the alkali is sodium hydroxide solution with the mass concentration of 5-30%, the reaction time is 1-5h, the reaction time in the second stage of impurity removal process is 1-5h, the calcium remover is oxalic acid, and the amount of the added calcium remover is 0.06% -0.1% of the electrolytic aluminum waste material.|6. The method for preparing battery grade lithium carbonate from electrolytic aluminum scrap according to claim 1, wherein the freezing crystallization temperature in step 5 is-10 ℃ to 10 ℃.|7. The method for preparing battery grade lithium carbonate from electrolytic aluminum scrap according to claim 1, wherein the heating temperature in step 6 is 90-100 ℃.|8. The method for preparing battery grade lithium carbonate by using electrolytic aluminum waste according to claim 1, wherein the mass ratio of pure water to crude lithium carbonate in the step 7 is 9-10:1, and the pressure of CO 2 gas is 0.1-0.2MPa.|9. The method for preparing battery grade lithium carbonate from electrolytic aluminum scrap according to claim 1, wherein the temperature of the heating crystallization in step 7 is 90-100 ℃. (CN119706889)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for preparing battery-grade lithium carbonate from electrolytic aluminum waste.|BACKGROUND ART|[0002] In recent years, the development of the electric automobile industry is well-developed, the rapid development of the lithium ion battery industry is driven, the demand of lithium raw materials is continuously increased, a plurality of companies lay out domestic and foreign lithium resources, the development of lithium extraction technology is carried out, the production of lithium carbonate is focused, the price of a lithium product is increased by a plurality of times compared with that of the prior product, and the price of the lithium raw materials is increased. At present, spodumene, lepidolite and other ores are mainly used for extracting or extracting lithium from salt lakes to prepare lithium carbonate.|[0003] Development of industries such as automobiles drives the growth of nonferrous metal demands, the electrolytic aluminum industry expands in batches, electrolytic aluminum waste residues contain a certain amount of lithium, and the materials are high in impurity content, particularly high in aluminum content, difficult to process and high in processing cost. The value of lithium raw materials in this material has been continuously focused and studied in recent years.|[0004] In the prior art, chinese patent CN105293536A discloses a lithium extraction method of electrolytic aluminum waste residues, which comprises the steps of carrying out sulfation roasting reaction on lithium-containing electrolytic aluminum waste residues and concentrated sulfuric acid at 200-400 ℃, leaching a roasting product by water, filtering to obtain a lithium-containing solution, adding sodium carbonate into the lithium-containing solution to carry out alkaline hydrolysis at 20-40 ℃, adding water into filter residues, adding lime into the filter residues to carry out causticization reaction, filtering, introducing filtrate into CO 2 to carry out carbonization reaction, and then filtering, washing and drying to obtain battery-grade lithium carbonate. The product quality is excellent, and the added value is high. The method uses sulfating roasting process-water leaching precipitation-causticization-lithium precipitation to prepare battery grade lithium carbonate, and has the advantages of long flow, high reagent consumption, high energy consumption and large pollution. Chinese patent CN109179457A discloses a method for extracting lithium from electrolytic aluminum waste residue, which comprises the steps of reacting the electrolytic aluminum waste residue with concentrated sulfuric acid to obtain a mixture A, (2) dissolving the mixture A in water, filtering to obtain a filtrate B, slowly adding calcium oxide into the filtrate B, filtering the obtained solution to obtain a filter residue C and a filtrate D, (3) heating the filtrate D, evaporating and concentrating the filtrate D, filtering, further evaporating and concentrating the filtrate to obtain a filtrate E, maintaining the filtrate E in a heated state, (4) adding saturated sodium carbonate solution into the filtrate E to obtain a suspension F, filtering the suspension F to obtain a filter cake, and washing and drying the filter cake to obtain a lithium carbonate product. The method adopts the waste residue of the electrolytic aluminum industry as the raw material, the cost is lower than that of the lithium ore raw material, the extraction is easy, the price of other raw materials used in the extraction method is low, the cost is low, the obtained byproducts can be recycled, but the method has long treatment flow and great difficulty aiming at the waste residue of the electrolytic aluminum with higher carbon and iron content.|DISCLOSURE|Disclosure of Invention|[0005] Therefore, in order to solve the problems of long flow, high energy consumption and the like in the prior art, the invention provides a method for preparing battery grade lithium carbonate by using electrolytic aluminum waste aiming at the electrolytic aluminum waste with higher carbon content and aluminum content, which comprises the following specific scheme:|[0006] a method for preparing battery grade lithium carbonate by electrolyzing aluminum scraps, which comprises the following steps: |[0007] step 1, crushing electrolytic aluminum waste with carbon content more than 50%, aluminum content 5-7 times of lithium content and iron content at least 2 times of lithium content; |[0008] Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and finely grinding to obtain a decarbonized material by adsorbing magnetic substances therein by a magnetic remover; |[0009] Step 3, carrying out two-stage leaching on the decarbonized material, controlling the pH value of the first-stage leaching to be 1.3-1.6, filtering the first-stage leaching to obtain a first-stage leaching solution and a first-stage leaching residue, carrying out two-stage leaching on the first-stage leaching residue, controlling the pH value of the second-stage leaching to be 0.5-1.0 to obtain a second-stage leaching solution and a second-stage leaching residue, and returning the second-stage leaching solution to the first-stage leaching process; |[0010] Step 4, performing two-stage impurity removal, wherein the one-stage impurity removal process comprises the steps of adding an oxidant into the first-stage leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues; |[0011] Step 5, heating and concentrating the filtrate containing lithium, and then freezing and crystallizing to obtain a denitration liquid; |[0012] Step 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate; |[0013] And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. |[0014] Further, the electrolytic aluminum scraps in the step 1 comprise, by mass, 1% -1.2% of lithium, 5.5% -6.6% of aluminum, 9.5% -10.0% of sodium, 2.2% -2.5% of iron, 1.0% -1.3% of calcium, 0.24% -0.26% of magnesium, 2.5% -2.9% of silicon, 6.0% -6.5% of fluorine, 0.14% -0.15% of sulfur, 0.1% of manganese, 50% of carbon and the balance of water.|[0015] Further, the size of the crushed electrolytic aluminum scraps in the step 1 is 1-10cm.|[0016] Further, in the leaching process in the step 3, the leaching agent is sulfuric acid with the mass fraction of 98%, the leaching temperature is 60-90 ℃, the leaching time is 1-5h, wherein the slurry liquid-solid ratio of water to carbon-removed materials in the first stage leaching is 3-10:1, the slurry liquid-solid ratio of the second stage leaching is 2-5:1, and the washing liquid is returned to the first stage leaching after washing the second stage leaching slag.|[0017] Further, the oxidant in the first stage of impurity removal in the step 4 is air, the impurity removal temperature is 55-70 ℃, alkali is sodium hydroxide solution with the mass concentration of 5-30%, the reaction time is 1-5h, the reaction time in the second stage of impurity removal is 1-5h, the calcium removing agent is oxalic acid, and the amount of the added calcium removing agent is 0.06% -0.1% of that of the electrolytic aluminum waste.|[0018] Further, the temperature of the freeze crystallization in the step 5 is-10 ℃ to 10 ℃.|[0019] Further, the heating temperature in step 6 is 90-100 ℃.|[0020] Further, in the step 7, the mass ratio of the pure water to the crude lithium carbonate is 9-10:1, and the pressure of the CO 2 gas is 0.1-0.2MPa.|[0021] Further, the temperature of the heating crystallization in the step 7 is 90-100 ℃.|[0022] Compared with the prior art, the invention has the following advantages:|[0023] (1) The electrolytic aluminum waste residue is firstly calcined at the temperature of more than 550 ℃, so that the lithium extraction treatment capacity can be improved by almost one time, the output of the same reaction kettle can be increased by one time, the concentration of lithium solution can be improved by about one time, the leached slag amount can be reduced by one half, the treatment difficulty and cost are greatly reduced, and the lithium recovery rate and the treatment efficiency are improved. |[0024] (2) The invention removes magnetic substances such as iron in materials through a demagnetizer, reduces the material treatment capacity, removes most of iron at the same time, reduces the acid consumption in the leaching process, can maintain the pH in a lower range in the leaching process, ensures the full leaching of lithium and does not need to consider the leaching of a large amount of iron, and simultaneously controls the pH of one section of impurity removal to be not more than 5, so that the product of one section of impurity removal is mainly aluminum hydroxide instead of a mixture of iron and aluminum precipitation, and purer aluminum hydroxide precipitate slag can be used as raw materials for preparing aluminum and other compounds of aluminum, such as alumina, cryolite and the like or as raw materials for aluminum smelting after calcination.|[0025] (3) The invention adopts two sections of normal pressure leaching, improves the leaching rate of lithium as much as possible by controlling the leaching conditions, and has the advantages of leaching condition mildness, no high temperature and high pressure condition, high safety coefficient, low treatment cost and easy operation, and the leaching rate of lithium can reach more than 99 percent.|[0026] (4) In addition, oxalic acid is used as a decalcifying agent instead of conventional ion exchange resin in the two-stage impurity removal process, so that excessive waste water can be avoided, the problem that the ion exchange resin is easy to scale in a sulfuric acid system is avoided, and the high-efficiency decalcifying and smooth system operation can be realized.|[0027] (5) The lithium solution after impurity removal of the material has higher sodium content, high denitration rate through low-temperature crystallization and low sodium ion concentration after denitration. The lithium solution after denitration is prepared into battery grade lithium carbonate by a conventional method, and the process is simple and the cost is low.|[0028] The method does not need to add special reagents or introduce impurity elements in the process, can effectively extract lithium in the electrolytic aluminum waste residue to prepare battery-grade lithium carbonate, and has high added value and good economic benefit.|DRAWINGS DESCRIPTION|[0029] Embodiments of the invention are further described below with reference to the accompanying drawings, in which:|[0030] fig. 1 shows a process flow diagram of the present invention. |INVENTION MODE|Detailed Description|[0031] In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail by the following examples with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0032] A method for preparing battery grade lithium carbonate by electrolyzing aluminum scraps, which comprises the following steps:|[0033] Step 1, crushing electrolytic aluminum waste with carbon content more than 50%, aluminum content 5-7 times and iron content at least 2 times of the lithium content, wherein the size of the crushed electrolytic aluminum waste is 1-10cm, lithium is 1% -1.2%, aluminum is 5.5-6.6%, sodium is 9.5-10.0%, iron is 2.2-2.5%, calcium is 1.0-1.3%, magnesium is 0.24-0.26%, silicon is 2.5-2.9%, fluorine is 6.0-6.5%, sulfur is 0.14-0.15%, manganese is <0.1%, carbon is >50%, and the balance is water. |[0034] Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and finely grinding to obtain a decarbonized material by adsorbing magnetic substances therein by a magnetic remover;|[0035] The method comprises the steps of carrying out two-stage leaching on a carbon-removed material, controlling the pH value of the first-stage leaching to be 1.3-1.6, filtering the first-stage leaching to obtain a first-stage leaching solution and a first-stage leaching residue, carrying out two-stage leaching on the first-stage leaching residue, controlling the pH value of the second-stage leaching to be 0.5-1.0, obtaining a second-stage leaching solution and a second-stage leaching residue, returning the second-stage leaching solution to the first-stage leaching process, wherein the slurry liquid-solid ratio in the leaching process is 3-10:1, the leaching agent is sulfuric acid with the mass fraction of 98%, the leaching temperature is 60-90 ℃, the leaching time is 1-5h, the liquid-solid ratio of the second-stage leaching is 2-5:1, the leaching time is 1-5h, and returning the washed liquid to the first-stage leaching after the second-stage leaching residue is washed. |[0036] Step 4, performing two-stage impurity removal, wherein the one-stage impurity removal process comprises the steps of adding an oxidant into the one-stage leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues, wherein the oxidant in the one-stage impurity removal process is air, the impurity removal temperature is 55-70 ℃, the alkali is sodium hydroxide solution with the mass concentration of 5-30%, and the reaction time is 1-5h;|[0037] Al2(SO4)3+6NaOH→3Na2SO4+2Al(OH)3↓|[0038] The second stage of impurity removing process includes adding calcium removing agent into filtrate, adding alkali to regulate pH value to 12.0-13.0, filtering to obtain lithium-containing filtrate and impurity filtering residue, and the second stage of impurity removing process has reaction time of 1-5 hr, calcium removing agent is oxalic acid and the amount of added calcium removing agent is 0.06-0.1% of the electrolytic aluminum waste. |[0039] Mn2++2NaOH→2Na++Mn(OH)2↓|[0040] H2C2O4+Ca2+→CaC2O4↓+2H+|[0041] Mg2++2NaOH→2Na++Mg(OH)2↓|[0042] And 5, heating and concentrating the lithium-containing filtrate, and then performing freezing crystallization to obtain a denitration liquid, wherein the temperature of the freezing crystallization is-10 ℃ to-10 ℃, and removing sodium sulfate.|[0043] And 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate, wherein the heating temperature is 90-100 ℃.|[0044] Li2SO4+Na2CO3→Li2CO3↓+2Na2SO4|[0045] And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. The mass ratio of the pure water to the crude lithium carbonate is 9-10:1, the pressure of the CO 2 gas is 0.1-0.2MPa, and the temperature of heating crystallization is 90-100 ℃.|[0046] Specific examples are as follows:|[0047] The electrolytic aluminum waste residue used in the following examples is in the form of hard block, the carbon content is more than 50%, and the main components of the materials are shown in Table 1. |[0048] TABLE 1 electrolytic aluminum slag content|[0049] |[0050] The raw material contains 1.17% of lithium, wherein the aluminum content is 6.441, 5.5 times of the lithium content, and the iron content is about 2 times of the lithium content. The material has low silicon content, high fluorine content, small amount of sulfur and carbon content over 50%.|[0051] Example 1|[0052] (1) 1500G of electrolytic aluminum waste is coarsely crushed into small blocks of about 1 cm to 10 cm.|[0053] (2) And (3) decarbonizing, namely placing 1000g of crushed materials into a calciner, heating and calcining at 550 ℃ for 5 hours, cooling, finely grinding, sieving with a 60-mesh sieve for standby, and adsorbing magnetic substances by using a demagnetizer to obtain the decarbonized materials.|[0054] (3) Mixing and stirring the carbon removal material and water in a solid-liquid ratio of 10:1 uniformly, adding 98% sulfuric acid, heating in a water bath at 80 ℃ to perform primary leaching, adding sulfuric acid to adjust the pH value to 1.3, leaching for 1h, filtering after leaching to obtain primary leaching solution and primary leaching slag, pulping the primary leaching slag and sulfuric acid in a solid-liquid ratio of 2:1, performing secondary leaching, leaching at a final pH value of 0.8, leaching for 1h, filtering after leaching to obtain secondary leaching solution and secondary leaching slag, washing the secondary leaching slag twice, performing subsequent treatment on the primary leaching solution, combining the washing water of the secondary leaching solution and the secondary leaching slag, performing primary leaching pulping or leaching, connecting an absorption device with the leaching kettle, wherein the absorption liquid is pure water, the absorption of HF gas generated in the leaching process, the lithium leaching rate is 98.78%, the iron leaching rate is 99.05%, and the aluminum leaching rate is 29.77%.|[0055] (4) The first stage leaching solution is subjected to two-stage impurity removal, wherein the first stage impurity removal is that 5% sodium hydroxide is added to the first stage leaching solution after air is introduced for 20min to adjust the pH value to 4.5, the reaction temperature is kept at 60 ℃, the reaction time is 4h, the filter liquor and the filter residue are obtained after filtration, the filter residue is pulped and washed twice, the filter liquor is subjected to two-stage impurity removal, 1g of calcium removing agent oxalic acid is added, then 5% sodium hydroxide is added to adjust the pH value to 12.0, the reaction time is 3h, the filter liquor and the filter residue containing lithium and impurities are obtained after filtration, and the filter residue is piled up.|[0056] (5) Concentrating and denitrating, namely heating and concentrating the filtrate containing lithium, cooling to 5 ℃,0 ℃ and minus 5 ℃ and carrying out three-stage freezing and crystallizing of sodium sulfate to obtain the liquid after denitration.|[0057] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at 90 ℃ to obtain crude lithium carbonate.|[0058] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.1MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0059] Example 2|[0060] (1) 5000G of electrolytic aluminum scraps are coarsely crushed into small blocks of about 5 cm to 10 cm.|[0061] (2) And (3) placing 4000g of the roughly broken material into a crucible, placing the crucible into a calciner, calcining at 1000 ℃ for 3 hours, finely grinding the material, sieving with a 100-mesh sieve for later use, and adsorbing magnetic substances by using a demagnetizer to obtain the decarbonized material.|[0062] (3) Mixing and stirring the decarbonized material and water in a solid-liquid ratio of 5:1 uniformly, adding 98% sulfuric acid, heating in a water bath at 70 ℃ for one-stage leaching, adding sulfuric acid to adjust the pH value to 1.5, leaching for 2.5h, filtering after leaching to obtain one-stage leaching solution and one-stage leaching slag, pulping the one-stage leaching slag and the sulfuric acid in a solid ratio of 5:1, performing secondary leaching, leaching with a final pH value of 0.5, leaching for 2.5h, filtering after leaching to obtain two-stage leaching solution and two-stage leaching slag, washing the two-stage leaching slag twice, performing subsequent treatment on the one-stage leaching solution, combining the two-stage leaching solution and the washing water of the two-stage leaching slag, performing one-stage leaching pulping or leaching, connecting an absorption device by a leaching kettle, wherein the absorption liquid is pure water, the HF gas generated in the leaching process is absorbed, the lithium leaching rate is 98.44%, the iron leaching rate is 99.25%, and the aluminum leaching rate is 31.25%.|[0063] (4) The first stage leaching solution is subjected to two-stage impurity removal, wherein the first stage impurity removal comprises the steps of introducing air into the first stage leaching solution for 30min, adding 20% sodium hydroxide to adjust the pH value to 5.0, keeping the reaction temperature to 70 ℃, reacting for 1h, filtering to obtain filtrate and filter residues, pulping and washing the filter residues twice, performing two-stage impurity removal on the filtrate, adding 3g of calcium removing agent oxalic acid, adding 20% sodium hydroxide to adjust the pH value to 12.0, reacting for 1h, filtering to obtain filtrate containing lithium and filter residues containing impurities, and piling the filter residues;|[0064] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, and freezing and crystallizing sodium sulfate in three stages to obtain the denitrated liquid. |[0065] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at the temperature of 95 ℃ to obtain crude lithium carbonate.|[0066] (7) Adding 9 times of pure water into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.2MPa, performing precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0067] Example 3|[0068] (1) The electrolytic aluminum waste 16kg is roughly crushed into small blocks of about 5 cm to 10 cm.|[0069] (2) And (3) putting 15kg of the roughly broken material into a crucible, placing the crucible into a calciner, calcining at 1600 ℃ for 0.5h, finely grinding the material, sieving with a 200-mesh sieve for later use, and adsorbing magnetic substances by using a demagnetizer to obtain the decarbonized material.|[0070] (3) Mixing and stirring the carbon removal material and water in a solid-liquid ratio of 3:1 uniformly, adding 98% sulfuric acid, heating in a water bath at 90 ℃ to perform primary leaching, adding sulfuric acid to adjust the pH value to 1.3, leaching for 5 hours, filtering after leaching to obtain primary leaching liquid and primary leaching slag, pulping the primary leaching slag and sulfuric acid in a solid-liquid ratio of 3:1, performing secondary leaching, leaching for 5 hours at a final pH value of 1.0, filtering after leaching to obtain secondary leaching liquid and secondary leaching slag, washing the secondary leaching slag twice, performing subsequent treatment on the primary leaching liquid, combining the washing water of the secondary leaching liquid and the secondary leaching slag, performing primary leaching pulping or leaching, connecting an absorption device with the leaching kettle, wherein the absorption liquid is pure water, the absorption of HF gas generated in the leaching process, the lithium leaching rate is 98.11%, the iron leaching rate is 98.85%, and the aluminum leaching rate is 25.65%.|[0071] (4) The first stage leaching solution is subjected to two-stage impurity removal, wherein the first stage impurity removal is that air is introduced into the first stage leaching solution for 60min, 30% sodium hydroxide is added to adjust the pH value to 5.0, the reaction temperature is kept at 70 ℃, the reaction time is 5h, the filter liquor and the filter residue are obtained after filtration, the filter residue is pulped and washed twice, the second stage impurity removal is carried out on the filter liquor, 15g of calcium removing agent oxalic acid is added, then 30% sodium hydroxide is added to adjust the pH value to 13.0, the reaction time is 5h, the filter liquor and the filter residue containing lithium and impurities are obtained after filtration, and the filter residue is piled up.|[0072] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, and freezing and crystallizing sodium sulfate in three stages to obtain the denitrated liquid.|[0073] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at 98 ℃ to obtain crude lithium carbonate.|[0074] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.2MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0075] Table 1 composition of final lithium carbonate product in examples|[0076] |[0077] While certain exemplary embodiments of the present application have been described above, it should be understood that they have been presented by way of example only, and not limitation, to the scope of the application. The features of these embodiments may be recombined in a suitable manner while still obtaining a solution that is within the scope of the application as claimed. Based on the above embodiments, all other embodiments obtained by those skilled in the art without making creative efforts, i.e., all modifications, equivalents, improvements etc., which are within the spirit and principles of the present application, fall within the protection scope of the present application as claimed. (CN119706889)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for preparing battery-grade lithium carbonate from electrolytic aluminum waste.|BACKGROUND ART|[0002] In recent years, the development of the electric automobile industry is well-developed, the rapid development of the lithium ion battery industry is driven, the demand of lithium raw materials is continuously increased, a plurality of companies lay out domestic and foreign lithium resources, the development of lithium extraction technology is carried out, the production of lithium carbonate is focused, the price of a lithium product is increased by a plurality of times compared with that of the prior product, and the price of the lithium raw materials is increased. At present, spodumene, lepidolite and other ores are mainly used for extracting or extracting lithium from salt lakes to prepare lithium carbonate.|[0003] Development of industries such as automobiles drives the growth of nonferrous metal demands, the electrolytic aluminum industry expands in batches, electrolytic aluminum waste residues contain a certain amount of lithium, and the materials are high in impurity content, particularly high in aluminum content, difficult to process and high in processing cost. The value of lithium raw materials in this material has been continuously focused and studied in recent years.|[0004] In the prior art, chinese patent CN105293536A discloses a lithium extraction method of electrolytic aluminum waste residues, which comprises the steps of carrying out sulfation roasting reaction on lithium-containing electrolytic aluminum waste residues and concentrated sulfuric acid at 200-400 ℃, leaching a roasting product by water, filtering to obtain a lithium-containing solution, adding sodium carbonate into the lithium-containing solution to carry out alkaline hydrolysis at 20-40 ℃, adding water into filter residues, adding lime into the filter residues to carry out causticization reaction, filtering, introducing filtrate into CO 2 to carry out carbonization reaction, and then filtering, washing and drying to obtain battery-grade lithium carbonate. The product quality is excellent, and the added value is high. The method uses sulfating roasting process-water leaching precipitation-causticization-lithium precipitation to prepare battery grade lithium carbonate, and has the advantages of long flow, high reagent consumption, high energy consumption and large pollution. Chinese patent CN109179457A discloses a method for extracting lithium from electrolytic aluminum waste residue, which comprises the steps of reacting the electrolytic aluminum waste residue with concentrated sulfuric acid to obtain a mixture A, (2) dissolving the mixture A in water, filtering to obtain a filtrate B, slowly adding calcium oxide into the filtrate B, filtering the obtained solution to obtain a filter residue C and a filtrate D, (3) heating the filtrate D, evaporating and concentrating the filtrate D, filtering, further evaporating and concentrating the filtrate to obtain a filtrate E, maintaining the filtrate E in a heated state, (4) adding saturated sodium carbonate solution into the filtrate E to obtain a suspension F, filtering the suspension F to obtain a filter cake, and washing and drying the filter cake to obtain a lithium carbonate product. The method adopts the waste residue of the electrolytic aluminum industry as the raw material, the cost is lower than that of the lithium ore raw material, the extraction is easy, the price of other raw materials used in the extraction method is low, the cost is low, the obtained byproducts can be recycled, but the method has long treatment flow and great difficulty aiming at the waste residue of the electrolytic aluminum with higher carbon and iron content.|DISCLOSURE|Disclosure of Invention|[0005] Therefore, in order to solve the problems of long flow, high energy consumption and the like in the prior art, the invention provides a method for preparing battery grade lithium carbonate by using electrolytic aluminum waste aiming at the electrolytic aluminum waste with higher carbon content and aluminum content, which comprises the following specific scheme:|[0006] a method for preparing battery grade lithium carbonate by electrolyzing aluminum scraps, which comprises the following steps: |[0007] step 1, crushing electrolytic aluminum waste with carbon content more than 50%, aluminum content 5-7 times of lithium content and iron content at least 2 times of lithium content; |[0008] Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and finely grinding to obtain a decarbonized material by adsorbing magnetic substances therein by a magnetic remover; |[0009] Step 3, carrying out two-stage leaching on the decarbonized material, controlling the pH value of the first-stage leaching to be 1.3-1.6, filtering the first-stage leaching to obtain a first-stage leaching solution and a first-stage leaching residue, carrying out two-stage leaching on the first-stage leaching residue, controlling the pH value of the second-stage leaching to be 0.5-1.0 to obtain a second-stage leaching solution and a second-stage leaching residue, and returning the second-stage leaching solution to the first-stage leaching process; |[0010] Step 4, performing two-stage impurity removal, wherein the one-stage impurity removal process comprises the steps of adding an oxidant into the first-stage leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues; |[0011] Step 5, heating and concentrating the filtrate containing lithium, and then freezing and crystallizing to obtain a denitration liquid; |[0012] Step 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate; |[0013] And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. |[0014] Further, the electrolytic aluminum scraps in the step 1 comprise, by mass, 1% -1.2% of lithium, 5.5% -6.6% of aluminum, 9.5% -10.0% of sodium, 2.2% -2.5% of iron, 1.0% -1.3% of calcium, 0.24% -0.26% of magnesium, 2.5% -2.9% of silicon, 6.0% -6.5% of fluorine, 0.14% -0.15% of sulfur, 0.1% of manganese, 50% of carbon and the balance of water.|[0015] Further, the size of the crushed electrolytic aluminum scraps in the step 1 is 1-10cm.|[0016] Further, in the leaching process in the step 3, the leaching agent is sulfuric acid with the mass fraction of 98%, the leaching temperature is 60-90 ℃, the leaching time is 1-5h, wherein the slurry liquid-solid ratio of water to carbon-removed materials in the first stage leaching is 3-10:1, the slurry liquid-solid ratio of the second stage leaching is 2-5:1, and the washing liquid is returned to the first stage leaching after washing the second stage leaching slag.|[0017] Further, the oxidant in the first stage of impurity removal in the step 4 is air, the impurity removal temperature is 55-70 ℃, alkali is sodium hydroxide solution with the mass concentration of 5-30%, the reaction time is 1-5h, the reaction time in the second stage of impurity removal is 1-5h, the calcium removing agent is oxalic acid, and the amount of the added calcium removing agent is 0.06% -0.1% of that of the electrolytic aluminum waste.|[0018] Further, the temperature of the freeze crystallization in the step 5 is-10 ℃ to 10 ℃.|[0019] Further, the heating temperature in step 6 is 90-100 ℃.|[0020] Further, in the step 7, the mass ratio of the pure water to the crude lithium carbonate is 9-10:1, and the pressure of the CO 2 gas is 0.1-0.2MPa.|[0021] Further, the temperature of the heating crystallization in the step 7 is 90-100 ℃.|[0022] Compared with the prior art, the invention has the following advantages:|[0023] (1) The electrolytic aluminum waste residue is firstly calcined at the temperature of more than 550 ℃, so that the lithium extraction treatment capacity can be improved by almost one time, the output of the same reaction kettle can be increased by one time, the concentration of lithium solution can be improved by about one time, the leached slag amount can be reduced by one half, the treatment difficulty and cost are greatly reduced, and the lithium recovery rate and the treatment efficiency are improved. |[0024] (2) The invention removes magnetic substances such as iron in materials through a demagnetizer, reduces the material treatment capacity, removes most of iron at the same time, reduces the acid consumption in the leaching process, can maintain the pH in a lower range in the leaching process, ensures the full leaching of lithium and does not need to consider the leaching of a large amount of iron, and simultaneously controls the pH of one section of impurity removal to be not more than 5, so that the product of one section of impurity removal is mainly aluminum hydroxide instead of a mixture of iron and aluminum precipitation, and purer aluminum hydroxide precipitate slag can be used as raw materials for preparing aluminum and other compounds of aluminum, such as alumina, cryolite and the like or as raw materials for aluminum smelting after calcination.|[0025] (3) The invention adopts two sections of normal pressure leaching, improves the leaching rate of lithium as much as possible by controlling the leaching conditions, and has the advantages of leaching condition mildness, no high temperature and high pressure condition, high safety coefficient, low treatment cost and easy operation, and the leaching rate of lithium can reach more than 99 percent.|[0026] (4) In addition, oxalic acid is used as a decalcifying agent instead of conventional ion exchange resin in the two-stage impurity removal process, so that excessive waste water can be avoided, the problem that the ion exchange resin is easy to scale in a sulfuric acid system is avoided, and the high-efficiency decalcifying and smooth system operation can be realized.|[0027] (5) The lithium solution after impurity removal of the material has higher sodium content, high denitration rate through low-temperature crystallization and low sodium ion concentration after denitration. The lithium solution after denitration is prepared into battery grade lithium carbonate by a conventional method, and the process is simple and the cost is low.|[0028] The method does not need to add special reagents or introduce impurity elements in the process, can effectively extract lithium in the electrolytic aluminum waste residue to prepare battery-grade lithium carbonate, and has high added value and good economic benefit.|DRAWINGS DESCRIPTION|[0029] Embodiments of the invention are further described below with reference to the accompanying drawings, in which:|[0030] fig. 1 shows a process flow diagram of the present invention. |INVENTION MODE|Detailed Description|[0031] In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail by the following examples with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0032] A method for preparing battery grade lithium carbonate by electrolyzing aluminum scraps, which comprises the following steps:|[0033] Step 1, crushing electrolytic aluminum waste with carbon content more than 50%, aluminum content 5-7 times and iron content at least 2 times of the lithium content, wherein the size of the crushed electrolytic aluminum waste is 1-10cm, lithium is 1% -1.2%, aluminum is 5.5-6.6%, sodium is 9.5-10.0%, iron is 2.2-2.5%, calcium is 1.0-1.3%, magnesium is 0.24-0.26%, silicon is 2.5-2.9%, fluorine is 6.0-6.5%, sulfur is 0.14-0.15%, manganese is <0.1%, carbon is >50%, and the balance is water. |[0034] Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and finely grinding to obtain a decarbonized material by adsorbing magnetic substances therein by a magnetic remover;|[0035] The method comprises the steps of carrying out two-stage leaching on a carbon-removed material, controlling the pH value of the first-stage leaching to be 1.3-1.6, filtering the first-stage leaching to obtain a first-stage leaching solution and a first-stage leaching residue, carrying out two-stage leaching on the first-stage leaching residue, controlling the pH value of the second-stage leaching to be 0.5-1.0, obtaining a second-stage leaching solution and a second-stage leaching residue, returning the second-stage leaching solution to the first-stage leaching process, wherein the slurry liquid-solid ratio in the leaching process is 3-10:1, the leaching agent is sulfuric acid with the mass fraction of 98%, the leaching temperature is 60-90 ℃, the leaching time is 1-5h, the liquid-solid ratio of the second-stage leaching is 2-5:1, the leaching time is 1-5h, and returning the washed liquid to the first-stage leaching after the second-stage leaching residue is washed. |[0036] Step 4, performing two-stage impurity removal, wherein the one-stage impurity removal process comprises the steps of adding an oxidant into the one-stage leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues, wherein the oxidant in the one-stage impurity removal process is air, the impurity removal temperature is 55-70 ℃, the alkali is sodium hydroxide solution with the mass concentration of 5-30%, and the reaction time is 1-5h;|[0037] Al2(SO4)3+6NaOH→3Na2SO4+2Al(OH)3↓|[0038] The second stage of impurity removing process includes adding calcium removing agent into filtrate, adding alkali to regulate pH value to 12.0-13.0, filtering to obtain lithium-containing filtrate and impurity filtering residue, and the second stage of impurity removing process has reaction time of 1-5 hr, calcium removing agent is oxalic acid and the amount of added calcium removing agent is 0.06-0.1% of the electrolytic aluminum waste. |[0039] Mn2++2NaOH→2Na++Mn(OH)2↓|[0040] H2C2O4+Ca2+→CaC2O4↓+2H+|[0041] Mg2++2NaOH→2Na++Mg(OH)2↓|[0042] And 5, heating and concentrating the lithium-containing filtrate, and then performing freezing crystallization to obtain a denitration liquid, wherein the temperature of the freezing crystallization is-10 ℃ to-10 ℃, and removing sodium sulfate.|[0043] And 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate, wherein the heating temperature is 90-100 ℃.|[0044] Li2SO4+Na2CO3→Li2CO3↓+2Na2SO4|[0045] And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. The mass ratio of the pure water to the crude lithium carbonate is 9-10:1, the pressure of the CO 2 gas is 0.1-0.2MPa, and the temperature of heating crystallization is 90-100 ℃.|[0046] Specific examples are as follows:|[0047] The electrolytic aluminum waste residue used in the following examples is in the form of hard block, the carbon content is more than 50%, and the main components of the materials are shown in Table 1. |[0048] TABLE 1 electrolytic aluminum slag content|[0049] |[0050] The raw material contains 1.17% of lithium, wherein the aluminum content is 6.441, 5.5 times of the lithium content, and the iron content is about 2 times of the lithium content. The material has low silicon content, high fluorine content, small amount of sulfur and carbon content over 50%.|[0051] Example 1|[0052] (1) 1500G of electrolytic aluminum waste is coarsely crushed into small blocks of about 1 cm to 10 cm.|[0053] (2) And (3) decarbonizing, namely placing 1000g of crushed materials into a calciner, heating and calcining at 550 ℃ for 5 hours, cooling, finely grinding, sieving with a 60-mesh sieve for standby, and adsorbing magnetic substances by using a demagnetizer to obtain the decarbonized materials.|[0054] (3) Mixing and stirring the carbon removal material and water in a solid-liquid ratio of 10:1 uniformly, adding 98% sulfuric acid, heating in a water bath at 80 ℃ to perform primary leaching, adding sulfuric acid to adjust the pH value to 1.3, leaching for 1h, filtering after leaching to obtain primary leaching solution and primary leaching slag, pulping the primary leaching slag and sulfuric acid in a solid-liquid ratio of 2:1, performing secondary leaching, leaching at a final pH value of 0.8, leaching for 1h, filtering after leaching to obtain secondary leaching solution and secondary leaching slag, washing the secondary leaching slag twice, performing subsequent treatment on the primary leaching solution, combining the washing water of the secondary leaching solution and the secondary leaching slag, performing primary leaching pulping or leaching, connecting an absorption device with the leaching kettle, wherein the absorption liquid is pure water, the absorption of HF gas generated in the leaching process, the lithium leaching rate is 98.78%, the iron leaching rate is 99.05%, and the aluminum leaching rate is 29.77%.|[0055] (4) The first stage leaching solution is subjected to two-stage impurity removal, wherein the first stage impurity removal is that 5% sodium hydroxide is added to the first stage leaching solution after air is introduced for 20min to adjust the pH value to 4.5, the reaction temperature is kept at 60 ℃, the reaction time is 4h, the filter liquor and the filter residue are obtained after filtration, the filter residue is pulped and washed twice, the filter liquor is subjected to two-stage impurity removal, 1g of calcium removing agent oxalic acid is added, then 5% sodium hydroxide is added to adjust the pH value to 12.0, the reaction time is 3h, the filter liquor and the filter residue containing lithium and impurities are obtained after filtration, and the filter residue is piled up.|[0056] (5) Concentrating and denitrating, namely heating and concentrating the filtrate containing lithium, cooling to 5 ℃,0 ℃ and minus 5 ℃ and carrying out three-stage freezing and crystallizing of sodium sulfate to obtain the liquid after denitration.|[0057] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at 90 ℃ to obtain crude lithium carbonate.|[0058] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.1MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0059] Example 2|[0060] (1) 5000G of electrolytic aluminum scraps are coarsely crushed into small blocks of about 5 cm to 10 cm.|[0061] (2) And (3) placing 4000g of the roughly broken material into a crucible, placing the crucible into a calciner, calcining at 1000 ℃ for 3 hours, finely grinding the material, sieving with a 100-mesh sieve for later use, and adsorbing magnetic substances by using a demagnetizer to obtain the decarbonized material.|[0062] (3) Mixing and stirring the decarbonized material and water in a solid-liquid ratio of 5:1 uniformly, adding 98% sulfuric acid, heating in a water bath at 70 ℃ for one-stage leaching, adding sulfuric acid to adjust the pH value to 1.5, leaching for 2.5h, filtering after leaching to obtain one-stage leaching solution and one-stage leaching slag, pulping the one-stage leaching slag and the sulfuric acid in a solid ratio of 5:1, performing secondary leaching, leaching with a final pH value of 0.5, leaching for 2.5h, filtering after leaching to obtain two-stage leaching solution and two-stage leaching slag, washing the two-stage leaching slag twice, performing subsequent treatment on the one-stage leaching solution, combining the two-stage leaching solution and the washing water of the two-stage leaching slag, performing one-stage leaching pulping or leaching, connecting an absorption device by a leaching kettle, wherein the absorption liquid is pure water, the HF gas generated in the leaching process is absorbed, the lithium leaching rate is 98.44%, the iron leaching rate is 99.25%, and the aluminum leaching rate is 31.25%.|[0063] (4) The first stage leaching solution is subjected to two-stage impurity removal, wherein the first stage impurity removal comprises the steps of introducing air into the first stage leaching solution for 30min, adding 20% sodium hydroxide to adjust the pH value to 5.0, keeping the reaction temperature to 70 ℃, reacting for 1h, filtering to obtain filtrate and filter residues, pulping and washing the filter residues twice, performing two-stage impurity removal on the filtrate, adding 3g of calcium removing agent oxalic acid, adding 20% sodium hydroxide to adjust the pH value to 12.0, reacting for 1h, filtering to obtain filtrate containing lithium and filter residues containing impurities, and piling the filter residues;|[0064] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, and freezing and crystallizing sodium sulfate in three stages to obtain the denitrated liquid. |[0065] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at the temperature of 95 ℃ to obtain crude lithium carbonate.|[0066] (7) Adding 9 times of pure water into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.2MPa, performing precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0067] Example 3|[0068] (1) The electrolytic aluminum waste 16kg is roughly crushed into small blocks of about 5 cm to 10 cm.|[0069] (2) And (3) putting 15kg of the roughly broken material into a crucible, placing the crucible into a calciner, calcining at 1600 ℃ for 0.5h, finely grinding the material, sieving with a 200-mesh sieve for later use, and adsorbing magnetic substances by using a demagnetizer to obtain the decarbonized material.|[0070] (3) Mixing and stirring the carbon removal material and water in a solid-liquid ratio of 3:1 uniformly, adding 98% sulfuric acid, heating in a water bath at 90 ℃ to perform primary leaching, adding sulfuric acid to adjust the pH value to 1.3, leaching for 5 hours, filtering after leaching to obtain primary leaching liquid and primary leaching slag, pulping the primary leaching slag and sulfuric acid in a solid-liquid ratio of 3:1, performing secondary leaching, leaching for 5 hours at a final pH value of 1.0, filtering after leaching to obtain secondary leaching liquid and secondary leaching slag, washing the secondary leaching slag twice, performing subsequent treatment on the primary leaching liquid, combining the washing water of the secondary leaching liquid and the secondary leaching slag, performing primary leaching pulping or leaching, connecting an absorption device with the leaching kettle, wherein the absorption liquid is pure water, the absorption of HF gas generated in the leaching process, the lithium leaching rate is 98.11%, the iron leaching rate is 98.85%, and the aluminum leaching rate is 25.65%.|[0071] (4) The first stage leaching solution is subjected to two-stage impurity removal, wherein the first stage impurity removal is that air is introduced into the first stage leaching solution for 60min, 30% sodium hydroxide is added to adjust the pH value to 5.0, the reaction temperature is kept at 70 ℃, the reaction time is 5h, the filter liquor and the filter residue are obtained after filtration, the filter residue is pulped and washed twice, the second stage impurity removal is carried out on the filter liquor, 15g of calcium removing agent oxalic acid is added, then 30% sodium hydroxide is added to adjust the pH value to 13.0, the reaction time is 5h, the filter liquor and the filter residue containing lithium and impurities are obtained after filtration, and the filter residue is piled up.|[0072] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, and freezing and crystallizing sodium sulfate in three stages to obtain the denitrated liquid.|[0073] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at 98 ℃ to obtain crude lithium carbonate.|[0074] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.2MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0075] Table 1 composition of final lithium carbonate product in examples|[0076] |[0077] While certain exemplary embodiments of the present application have been described above, it should be understood that they have been presented by way of example only, and not limitation, to the scope of the application. The features of these embodiments may be recombined in a suitable manner while still obtaining a solution that is within the scope of the application as claimed. Based on the above embodiments, all other embodiments obtained by those skilled in the art without making creative efforts, i.e., all modifications, equivalents, improvements etc., which are within the spirit and principles of the present application, fall within the protection scope of the present application as claimed. Family Number|(113961434)|113961434|Abstract|(CN119706889 A)|The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium - containing waste , in particular to a method for preparing battery - grade lithium carbonate from electrolytic aluminum waste . The method comprises the following steps : ( 1 ) coarsely crushing the electrolytic aluminum waste ; ( 2 ) calcining or combusting the coarsely crushed material to remove carbon , then performing fine grinding , and adsorbing magnetic substances by using a demagnetizer ; ( 3 ) leaching : carrying out two - stage leaching on the material subjected to carbon removal ; ( 4 ) impurity removal : performing two - stage impurity removal on the first - stage leachate ; and ( 5 ) carrying out concentration , denitration , lithium precipitation and refining on the lithium solution after impurity removal to prepare the battery - grade lithium carbonate . The electrolytic aluminum waste residues are firstly subjected to carbon removal , the lithium extraction treatment capacity and the leaching rate are improved , ferromagnetic substances in the raw materials are removed through a magnetic removal method , the use amount of leaching acid and the use amount of impurity removal oxidizing agents and alkali are reduced , the main component of impurity removal residues is aluminum hydroxide with high purity and can be directly utilized , the treatment difficulty and cost are greatly reduced , and the method is suitable for industrial production . The lithium recovery rate and the treatment efficiency are improved . |IPC codes|(CN119706889 A)|C01D - 015/08 | Materials, metallurgy C01D-015/08 C01D-015/08 PENDING (CN119706889)|PENDING ALIVE (CN119706889)|ALIVE (CN119706889)|LEGAL DETAILS FOR CN119706889|Actual or expected expiration date=2044-12-02|Legal state=ALIVE|Status=PENDING|Event publication date=2024-12-02|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202411750392|Application date=2024-12-02|Standardized application number=2024CN-1750392|Event publication date=2025-03-28|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119706889|Publication stage code=A|Publication date=2025-03-28|Standardized publication number=CN119706889|Event publication date=2025-03-28|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-04-15|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN119706889)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSDz4cGU9txV1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000076975620&ekey=2117&xpn=CN119706889&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=skx14qgEt5Cf%252FEqnE1z6ZpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN119706889)|CN (CN119706889)|NAME=JINCHUAN GROUP CO. LTD. , COUNTRY=CN (CN119706889)|NAME=LI ZIJIAN;CHINA NONFERROUS METALS INDUSTRY PATENT CENTER , REG=11028 (CN119706889)|NAME=CHAI GENFENG|NAME=HU JIAYAN|NAME=YANG XIAOYAN|NAME=WANG JUANHUI|NAME=XIE YI|NAME=HUO WENSHENG|NAME=HUANG SHUWEN|NAME=HE YAN|NAME=ZHANG JIALE|NAME=MA JIANJI|NAME=TANG PENGJUN 0 1 Titre: (CN119706889)|Method for preparing battery-grade lithium carbonate from electrolytic aluminum waste Résumé: (CN119706889)|The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for preparing battery-grade lithium carbonate from electrolytic aluminum waste. The method comprises the following steps: (1) coarsely crushing the electrolytic aluminum waste; (2) calcining or combusting the coarsely crushed material to remove carbon, then performing fine grinding, and adsorbing magnetic substances by using a demagnetizer; (3) leaching: carrying out two-stage leaching on the material subjected to carbon removal; (4) impurity removal: performing two-stage impurity removal on the first-stage leachate; and (5) carrying out concentration, denitration, lithium precipitation and refining on the lithium solution after impurity removal to prepare the battery-grade lithium carbonate. The electrolytic aluminum waste residues are firstly subjected to carbon removal, the lithium extraction treatment capacity and the leaching rate are improved, ferromagnetic substances in the raw materials are removed through a magnetic removal method, the use amount of leaching acid and the use amount of impurity removal oxidizing agents and alkali are reduced, the main component of impurity removal residues is aluminum hydroxide with high purity and can be directly utilized, the treatment difficulty and cost are greatly reduced, and the method is suitable for industrial production. The lithium recovery rate and the treatment efficiency are improved. 82 Abstract gpt-4o-mini no The article focuses on the extraction of lithium carbonate from aluminum waste, which does not relate to accelerated weathering or CO₂ capture.
83 CN202011240804 CN202011240804 CN112142537 92088576 CN112142537 A 2020-12-29 [CN112142537] 2020-11-09 2020-11-09 2020-12-29 (CN112142537)|2022-12-23 (CN112142537)|Biochar compound fertilizer as well as preparation method and application thereof (CN112142537)|The invention discloses a biochar compound fertilizer which comprises the following raw materials in parts by weight: 50-60 parts of biochar, 30-40 parts of livestock and poultry manure, 25-35 parts of bamboo powder, 20-30 parts of peanut shell powder, 5-10 parts of a binder and 0.8-1.5 parts of a complex microbial inoculant. The preparation method comprises the following steps: (1) weighing the raw materials; (2) mixing, crushing and sieving the biochar, the bamboo powder and the peanut shell powder; (3) mixing with livestock and poultry manure and the complex microbial inoculant, and fermenting; and (4) mixing with the binder, granulating and drying to obtain the biochar compound fertilizer. The biochar has the characteristics of being loose, porous, good in air permeability and water permeability, large in specific surface area and high in adsorption capacity and chelating capacity, and has the outstanding advantages of being safe, environmentally friendly, efficient and the like incooperation with other organic raw materials, and therefore the organic farmland soil fertility and the carbon sequestration and emission reduction capacity are effectively improved. INSTITUTE OF PLANT NUTITUION & RESOURCE ENVIRONMENT HENAN ACADEMY OF AGRICULTURAL SCIENCES (CN112142537)|INSTITUTE OF PLANT NUTITUION AND RESOURCE ENVIRONMENT, HENAN ACADEMY OF AGRICULTURAL SCIENCES ([CN]) DU JUN|YANG HUANHUAN|HU YING|HE AILING|PAN XIUYAN|XU JIDONG|LIU GAOYUAN (CN112142537)|DU JUN|YANG HUANHUAN|HU YING|HE AILING|PAN XIUYAN|XU JIDONG|LIU GAOYUAN (CN112142537)|ZHAO XUPING;MUDA INTELLECTUAL PROPERTY|Reg. Nb: 11465 (CN112142537)|The invention has the advantages that the biochar has the characteristics of looseness, porosity, good air and water permeability, large specific surface area, strong adsorption capacity and chelating capacity, and has the outstanding advantages of safety, environmental protection, high efficiency and the like by being matched with other organic matter raw materials, so that the fertility of organic farmland soil and the carbon sequestration and emission reduction capacity are effectively improved.|However, the existing method for using the biochar is generally to add organic and/or inorganic fertilizers for matching use, so that on one hand, the biochar is troublesome to use and high in cost, and on the other hand, the effect of the biochar is influenced, so that the biochar cannot fully play a role.| (CN112142537)|1. The biochar compound fertilizer is characterized by comprising the following raw materials in parts by weight: 50-60 parts of charcoal, 30-40 parts of livestock and poultry manure, 25-35 parts of bamboo powder, 20-30 parts of peanut shell powder, 5-10 parts of binder and 0.8-1.5 parts of composite microbial inoculum.| (CN112142537)|In view of the above, the present invention aims to provide a biochar compound fertilizer, a preparation method and an application thereof, so as to solve the defects in the prior art. In order to achieve the purpose, the invention adopts the following technical scheme:|The invention discloses a biochar compound fertilizer which comprises the following raw materials in parts by weight: 50-60 parts of charcoal, 30-40 parts of livestock and poultry manure, 25-35 parts of bamboo powder, 20-30 parts of peanut shell powder, 5-10 parts of binder and 0.8-1.5 parts of composite microbial inoculum; the preparation method comprises the following steps: (1) weighing the raw materials; (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving; (3) mixing with livestock and poultry manure and a complex microbial inoculum, and fermenting; (4) mixing with a binder, granulating and drying to obtain the biochar compound fertilizer.|The invention relates to the technical field of fertilizers, in particular to a biochar compound fertilizer and a preparation method and application thereof.| (CN112142537)|BIOCHAR COMPOUND FERTILIZER(100,52)|COMPOSITE MICROBIAL INOCULUM(81,17)|POULTRY MANURE(58,13)|BAMBOO POWDER(52,29)|ORGANIC FARMLAND SOIL FERTILITY(43,1)|COMPLEX MICROBIAL INOCULUM(39,1)|CRUSHED PLANT STRAW(30,19)|ORGANIC FARMLAND SOIL(29,1)|BIOCHAR(28,27)|ADSORPTION CAPACITY(26,2)|LIVESTOCK(25,13)|CHELATING CAPACITY(25,2)|INORGANIC FERTILIZER(25,1)|LIVESTOCK MANURE(24,1)|COMPOUND MICROBIAL INOCULUM(22,1)|BINDER(21,13)|PEANUT(20,22)|CARBONIZATION FURNACE(17,7)|WATER PERMEABILITY(17,2)|CHARCOAL(16,12)|DUCK MANURE(16,4)|HOG MANURE(16,4)|PLANTING WHEAT(16,2)|SHEEP MANURE(15,4)|FRIENDLINESS(15,1)|CRUSHING PLANT STRAW(13,7)|POROSITY(13,3)|CARBON SEQUESTRATION(13,2)|EMISSION REDUCTION CAPACITY(13,2)|SIEVING(12,2)|DEFECT(12,1)|ACTINOMYCETE(9,12)|FERTILIZER(9,4)|ENVIRONMENTAL PROTECTION(9,1)|BACILLUS SUBTILIS(8,12)|AZOMONA(8,9)|COW MANURE(8,2)|ATTAPULGITE(7,4)|CHICKEN MANURE(7,4)|SIEVED SCREEN NUMBER(7,1)|BIOCHAR COMPOUND FERTILIZER WEIGHT(6,5)|CROP RHIZOSPHERE ENVIRONMENT(6,2)|DRYING TEMPERATURE(6,2)|RAW MATERIAL(5,22)|CLAY(5,8)|ORGANIC MATTER(5,6)|STARCH(5,4)|NITROGEN MONAD(5,3)|PLANT STRAW COMPOSITE MATERIAL(5,2)|CORN(4,4)|BIOCHAR ORGANIC FERTILIZER(4,2)|CROP STRAW(4,2)|NYT REQUIREMENT(4,2)|ORGANIC MATTER RAW MATERIAL(4,2)|EXPERIMENTAL FERTILIZATION ZONE(4,1)|FARMLAND SOIL(4,1)|MAIZE STATISTICS(4,1)|RELIEVING CLIMATE WARMING(4,1)|SPIKE FERTILIZER(4,1)|TILLER FERTILIZER(4,1)|GRAIN WEIGHT(3,3)|EXPERIMENTAL FERTILIZATION AREA(3,2)|SOIL ENZYME ACTIVITY(3,2)|SOIL FERTILIZER STORAGE CAPACITY(3,2)|CREATIVE EFFORT(3,1)|DRYING GRANULATION(3,1)|FECAL COLIFORM COUNT(3,1)|WATER CONTENT(2,7)|COW DUNG(2,2)|FERMENTATION(2,2)|AGRICULTURAL ORGANIC(2,1)|BIOFERTILIZER MEASURING PROPERTY(2,1)|FARMLAND CARBON FIXATION CAPACITY(2,1)|FERTILIZATION MODE(2,1)|INORGANIC SUBSTANCE(2,1)|NUTRIENT ABSORPTION(2,1)|NUTRIENT SUBSTANCE(2,1)|SEEDLING SLOW FERTILIZER(2,1)|SIEVED MESH(2,1)|SOIL MOISTURE ACCUMULATION(2,1)|STAGE FERTILIZATION(2,1)| (CN112142537)|1. The biochar compound fertilizer is characterized by comprising the following raw materials in parts by weight: 50-60 parts of charcoal, 30-40 parts of livestock and poultry manure, 25-35 parts of bamboo powder, 20-30 parts of peanut shell powder, 5-10 parts of binder and 0.8-1.5 parts of composite microbial inoculum.|2. The biochar compound fertilizer as claimed in claim 1, which is characterized by comprising the following raw materials in parts by weight: 52-58 parts of charcoal, 32-36 parts of livestock and poultry manure, 28-32 parts of bamboo powder, 22-28 parts of peanut shell powder, 6-9 parts of binder and 0.8-1.2 parts of composite microbial inoculum.|3. The biochar compound fertilizer as claimed in claim 1, which is characterized by comprising the following raw materials in parts by weight: 55 parts of charcoal, 35 parts of livestock and poultry manure, 30 parts of bamboo powder, 25 parts of peanut shell powder, 8 parts of a binder and 1.0 part of a composite microbial inoculum.|4. The biochar compound fertilizer as claimed in any one of claims 1 to 3, wherein the livestock manure is at least one of pig manure, cow manure, sheep manure, chicken manure and duck manure.|5. The biochar compound fertilizer as claimed in any one of claims 1 to 3, wherein the binder is at least one of starch, clay and attapulgite.|6. The biochar compound fertilizer as claimed in any one of claims 1 to 3, wherein the compound microbial inoculum is prepared from (2-5): (1-4): and (1-2) mixing the bacillus subtilis, the actinomycetes and the azomonas.|7. The preparation method of the biochar compound fertilizer is characterized by comprising the following steps:|(1) weighing the raw materials according to the parts by weight of the biochar compound fertilizer as defined in any one of claims 1 to 6;|(2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving to obtain a material A;|(3) mixing the material A, the livestock and poultry manure and the composite microbial inoculum, and fermenting for 24-36h at 25-35 ℃ to obtain a material B;|(4) and mixing the material B with a binder, granulating and drying to obtain the biochar compound fertilizer.|8. The biochar compound fertilizer as claimed in claim 7, wherein the preparation method of the biochar is as follows: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2 to 3 hours at the temperature of between 550 and 600 ℃ under the protection of nitrogen, and cooling the plant straws to obtain the plant straw composite material.|9. The biochar compound fertilizer as claimed in claim 6, wherein in the step (2), the number of the sieved screens is 100-200 meshes;|in the step (4), the drying temperature is 50-60 ℃, and the drying is carried out until the water content is below 10%.|10. The application of the biochar compound fertilizer as defined in any one of claims 1 to 5 in planting wheat and corn, wherein the fertilizing amount of the biochar compound fertilizer is 60 to 80 kg/mu. (CN112142537)|TECHNICAL FIELD|[0002] The invention relates to the technical field of fertilizers, in particular to a biochar compound fertilizer and a preparation method and application thereof.|BACKGROUND ART|[0004] In the global warming background, agricultural organic wastes (such as crop straws, animal wastes and the like) are returned to the field and are considered as one of important measures for improving the soil carbon reservoir. Crop straws and animal wastes are allowed to be used in organic farmlands after being decomposed, however, the carbon rejection rate of the organic wastes in the farmland soil is only 2% -20% within one year, and the returning of the organic wastes to the field can also excite CH4Or N2And a large amount of greenhouse gas O is discharged, so that the carbon fixation and emission reduction potential of returning organic wastes to the field is greatly reduced. Therefore, how to improve the carbon fixation and emission reduction capability of the organic farmland applying organic fertilizer to maintain soil fertility has important significance for relieving climate warming.|[0005] Biochar is a carbon-rich, highly aromatic and highly stable organic substance produced by high-temperature thermal cracking (generally <700 ℃) of an organic material under the condition of complete or partial hypoxia, has obvious improvement effect on physical and chemical properties of soil, and has porous characteristic and larger specific surface area, which are beneficial to soil moisture accumulation, porosity improvement and volume weight reduction, thereby providing a good environment for plant growth. Meanwhile, the biochar is an ideal modifier for acid soil, nutrient elements contained in the biochar can be directly input into the soil, and surface charges and functional groups of the biochar are favorable for retaining soil nutrients.|[0006] The organic waste is converted into the biochar and returned to the field, and the carbon rejection rate per year is as high as more than 90%, so that the carbon fixation capacity of the farmland can be remarkably improved by returning the biochar to the field. However, the existing method for using the biochar is generally to add organic and/or inorganic fertilizers for matching use, so that on one hand, the biochar is troublesome to use and high in cost, and on the other hand, the effect of the biochar is influenced, so that the biochar cannot fully play a role. In addition, the existing biochar has a small microporous structure and a small specific surface area due to the raw materials and the preparation method, and the microporous structure and the specific surface area are one of the factors determining the main functions of the biochar. Moreover, because of the raw materials and the preparation method, the nutrient elements including trace elements reserved by the biochar are less, and the biochar is also one of the reasons that other fertilizers need to be added at present.|[0007] Therefore, the problem to be solved by the technical personnel in the field is how to provide the biochar compound fertilizer which is simple to prepare and convenient to use.|[0008] Disclosure of Invention|[0009] In view of the above, the present invention aims to provide a biochar compound fertilizer, a preparation method and an application thereof, so as to solve the defects in the prior art.|[0010] In order to achieve the purpose, the invention adopts the following technical scheme:|[0011] the biochar compound fertilizer comprises the following raw materials in parts by weight: 50-60 parts of charcoal, 30-40 parts of livestock and poultry manure, 25-35 parts of bamboo powder, 20-30 parts of peanut shell powder, 5-10 parts of binder and 0.8-1.5 parts of composite microbial inoculum;|[0012] preferably: 52-58 parts of charcoal, 32-36 parts of livestock and poultry manure, 28-32 parts of bamboo powder, 22-28 parts of peanut shell powder, 6-9 parts of binder and 0.8-1.2 parts of composite microbial inoculum;|[0013] more preferably: 55 parts of charcoal, 35 parts of livestock and poultry manure, 30 parts of bamboo powder, 25 parts of peanut shell powder, 8 parts of a binder and 1.0 part of a composite microbial inoculum.|[0014] The invention has the advantages that the biochar has the characteristics of looseness, porosity, good air and water permeability, large specific surface area, strong adsorption capacity and chelating capacity, and has the outstanding advantages of safety, environmental protection, high efficiency and the like by being matched with other organic matter raw materials, so that the fertility of organic farmland soil and the carbon sequestration and emission reduction capacity are effectively improved.|[0015] Further, the livestock and poultry manure is at least one of pig manure, cow manure, sheep manure, chicken manure and duck manure.|[0016] The livestock and poultry manure contains rich organic matters, nitrogen, phosphorus, potassium and other nutrients, and can supply various mineral substances and trace elements such as calcium, magnesium, sulfur and the like required by crops, so that the requirements of the crops on various nutrients in the growth process are met.|[0017] Further, the binder is at least one of starch, clay and attapulgite.|[0018] The further technical scheme has the beneficial effects that the binder disclosed by the invention can improve the granulation rate of the fertilizer, and the granule has high strength and is free from agglomeration and moisture regain.|[0019] Further, the composite microbial inoculum is prepared from (2-5) by weight: (1-4): and (1-2) mixing the bacillus subtilis, the actinomycetes and the azomonas.|[0020] The composite microbial inoculum has the beneficial effects that the composite microbial inoculum can fully decompose the biochar, the livestock and poultry manure, the bamboo powder and the peanut shell powder, organic matters generated after fermentation can increase soil gaps, water and air are kept, and nutrient substances are provided for crops.|[0021] A preparation method of a biochar compound fertilizer specifically comprises the following steps:|[0022] (1) weighing the raw materials according to the parts by weight of the biochar compound fertilizer;|[0023] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving to obtain a material A;|[0024] (3) mixing the material A, the livestock and poultry manure and the composite microbial inoculum, and fermenting for 24-36h at 25-35 ℃ to obtain a material B;|[0025] (4) and mixing the material B with a binder, granulating and drying to obtain the biochar compound fertilizer.|[0026] Further, the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2 to 3 hours at the temperature of between 550 and 600 ℃ under the protection of nitrogen, and cooling the plant straws to obtain the plant straw composite material.|[0027] The further technical scheme has the beneficial effects that the preparation condition of the biochar is mild, the biochar is simple and easy to operate, and the prepared biochar has excellent performance.|[0028] Furthermore, in the step (2), the mesh number of the sieved mesh is 100-200 meshes.|[0029] The method has the beneficial effects that the biochar, the bamboo powder and the peanut shell powder are prepared into smaller particles through crushing and sieving, so that the fermentation and granulation drying steps are convenient to carry out.|[0030] In the step (4), the drying temperature is 50-60 ℃, and the drying is carried out until the water content is below 10%.|[0031] The beneficial effect of adopting the further technical scheme is that the biochar compound fertilizer is granulated and dried, and the biochar compound fertilizer absorbs water to expand into powder when being used, so that the contact area of the biochar compound fertilizer and soil is increased, better nutrient absorption of crops is facilitated, and the growth of the crops is promoted.|[0032] The invention also provides application of the biochar compound fertilizer in planting wheat and corn, and the fertilizing amount is 60-80 kg/mu.|[0033] According to the technical scheme, compared with the prior art, the invention has the following beneficial effects:|[0034] the biochar compound fertilizer disclosed by the invention can increase the content of organic matters in soil, improve the structure and porosity of the soil, increase the water and fertilizer storage capacity of the soil, improve the rhizosphere environment of crops, improve the enzyme activity of the soil, promote the reproduction of beneficial microorganisms at the rhizosphere of the crops, make the root system grow robustly and improve the yield of the crops.|INVENTION MODE|[0035] Detailed Description|[0036] The technical solutions in the embodiments of the present invention are clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.|[0037] Example 1|[0038] The biochar compound fertilizer comprises the following raw materials in parts by weight: 50kg of charcoal, 30kg of pig manure, 25kg of bamboo powder, 20kg of peanut shell powder, 5kg of starch, 0.2kg of bacillus subtilis, 0.4kg of actinomycetes and 0.2kg of azomonas;|[0039] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0040] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2 hours at 550 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0041] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture through a 100-mesh sieve to obtain a material A;|[0042] (3) mixing the material A, pig manure, bacillus subtilis, actinomycetes and nitrogen monad, and fermenting for 24 hours at 25 ℃ to obtain a material B;|[0043] (4) and mixing the material B with starch, granulating, and drying at 50 ℃ until the water content is 10% to obtain the biochar compound fertilizer.|[0044] Example 2|[0045] The biochar compound fertilizer comprises the following raw materials in parts by weight: 52kg of charcoal, 32kg of cow dung, 28kg of bamboo powder, 22kg of peanut shell powder, 6kg of clay, 0.2kg of bacillus subtilis, 0.4kg of actinomycetes and 0.2kg of azomonas;|[0046] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0047] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2 hours at 560 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0048] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture through a 120-mesh sieve to obtain a material A;|[0049] (3) mixing the material A, cow dung, bacillus subtilis, actinomycetes and nitrogen monad, and fermenting for 28 hours at 28 ℃ to obtain a material B;|[0050] (4) and mixing the material B with clay, granulating, and drying at 52 ℃ until the water content is 10% to obtain the biochar compound fertilizer.|[0051] Example 3|[0052] The biochar compound fertilizer comprises the following raw materials in parts by weight: 55kg of charcoal, 35kg of chicken manure, 30kg of bamboo powder, 25kg of peanut shell powder, 8kg of clay, 0.5kg of bacillus subtilis, 0.4kg of actinomycetes and 0.1kg of azomonas;|[0053] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0054] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2.5 hours at 580 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0055] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture through a 150-mesh sieve to obtain a material A;|[0056] (3) mixing the material A, chicken manure, bacillus subtilis, actinomycetes and nitrogen monad, and fermenting for 30 hours at 30 ℃ to obtain a material B;|[0057] (4) and mixing the material B with clay, granulating, and drying at 55 ℃ until the water content is 6% to obtain the biochar compound fertilizer.|[0058] Example 4|[0059] The biochar compound fertilizer comprises the following raw materials in parts by weight: 58kg of charcoal, 36kg of sheep manure, 32kg of bamboo powder, 28kg of peanut shell powder, 9kg of clay, 0.4kg of bacillus subtilis, 0.4kg of actinomycetes and 0.4kg of azomonas;|[0060] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0061] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 3 hours at 580 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0062] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture through a 180-mesh sieve to obtain a material A;|[0063] (3) mixing the material A, sheep manure, bacillus subtilis, actinomycetes and azomonas, and fermenting for 32 hours at 32 ℃ to obtain a material B;|[0064] (4) and mixing the material B with clay, granulating, and drying at 58 ℃ until the water content is 8% to obtain the biochar compound fertilizer.|[0065] Example 5|[0066] The biochar compound fertilizer comprises the following raw materials in parts by weight: 60kg of charcoal, 40kg of duck manure, 35kg of bamboo powder, 30kg of peanut shell powder, 10kg of attapulgite, 0.6kg of bacillus subtilis, 0.6kg of actinomycetes and 0.3kg of azomonas;|[0067] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0068] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 3 hours at 600 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0069] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture by a 200-mesh sieve to obtain a material A;|[0070] (3) mixing the material A, duck manure, bacillus subtilis, actinomycetes and azomonas, and fermenting at 35 ℃ for 36 hours to obtain a material B;|[0071] (4) and mixing the material B and the attapulgite, granulating, and drying at 60 ℃ until the water content is 8% to obtain the biochar compound fertilizer.|[0072] Performance testing|[0073] 1. The biochar compound fertilizers prepared in the embodiments 1 to 5 are respectively taken and tested for effective viable count, organic matter, moisture, pH value, fecal coliform count and ascarid egg death rate according to the test method and requirements of NYT 3618-2020 biochar-based organic fertilizer.|[0074] The measurement results are shown in table 1.|[0075] Table 1 examples 1-3 results of measuring properties of biofertilizers|[0076] |[0077] As can be seen from Table 1, all indexes of the biochar compound fertilizer prepared by the embodiments 1-5 of the invention all meet the corresponding requirements of NYT 3618-2020 biochar-based organic fertilizer. Among them, example 3 is the most preferable example.|[0078] 2. Corn field test|[0079] Selecting a corn test field in Zhengzhou city in Henan province, averagely dividing the corn test field into two parts, recording the two parts as a conventional fertilization area and a test fertilization area, selecting Zhonghe 107 corn varieties, respectively counting the grain number of each ear, the thousand grain weight and the yield of the corn after the corn is mature, and calculating the yield increasing rate.|[0080] The specific fertilization method of the conventional fertilization area comprises the following steps: local conventional fertilization, namely respectively applying base fertilizer, seedling-slow fertilizer, tiller fertilizer and spike fertilizer for 4 times by adopting a stage fertilization method, wherein the fertilization amount and the fertilization mode are consistent with those of local agricultural production; the specific fertilization method of the experimental fertilization area comprises the following steps: 80kg of the biochar compound fertilizer prepared in the embodiment 3 is applied to each mu of land at one time in a base fertilizer mode, and other fertilizers are not applied additionally.|[0081] The statistical results are shown in table 2.|[0082] TABLE 2 statistics of maize in conventional and experimental fertilization zones|[0083] Measurement indexGrain number of spike (grain)Thousand Kernel weight (g)Yield (kg/mu)Conventional fertilization area481235.12445.63Experimental fertilization district584276.58536.88Yield increase (%)21.4117.6320.48|[0084] As can be seen from Table 2, the grain number per ear, the thousand grain weight and the yield of the corns in the experimental fertilization area are all superior to those in the conventional fertilization area, wherein the grain number per ear is increased by 21.41%, the thousand grain weight is increased by 17.63%, and the yield is increased by 20.48%.|[0085] The tests show that the biochar compound fertilizer can increase the content of organic matters in soil, improve the structure and porosity of the soil, increase the water and fertilizer storage capacity of the soil, improve the rhizosphere environment of crops, improve the enzyme activity of the soil, promote the multiplication of beneficial microorganisms in the rhizosphere of the crops, make the root systems grow healthily and improve the yield of the crops.|[0086] The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. (CN112142537)|TECHNICAL FIELD|[0002] The invention relates to the technical field of fertilizers, in particular to a biochar compound fertilizer and a preparation method and application thereof.|BACKGROUND ART|[0004] In the global warming background, agricultural organic wastes (such as crop straws, animal wastes and the like) are returned to the field and are considered as one of important measures for improving the soil carbon reservoir. Crop straws and animal wastes are allowed to be used in organic farmlands after being decomposed, however, the carbon rejection rate of the organic wastes in the farmland soil is only 2% -20% within one year, and the returning of the organic wastes to the field can also excite CH4Or N2And a large amount of greenhouse gas O is discharged, so that the carbon fixation and emission reduction potential of returning organic wastes to the field is greatly reduced. Therefore, how to improve the carbon fixation and emission reduction capability of the organic farmland applying organic fertilizer to maintain soil fertility has important significance for relieving climate warming.|[0005] Biochar is a carbon-rich, highly aromatic and highly stable organic substance produced by high-temperature thermal cracking (generally <700 ℃) of an organic material under the condition of complete or partial hypoxia, has obvious improvement effect on physical and chemical properties of soil, and has porous characteristic and larger specific surface area, which are beneficial to soil moisture accumulation, porosity improvement and volume weight reduction, thereby providing a good environment for plant growth. Meanwhile, the biochar is an ideal modifier for acid soil, nutrient elements contained in the biochar can be directly input into the soil, and surface charges and functional groups of the biochar are favorable for retaining soil nutrients.|[0006] The organic waste is converted into the biochar and returned to the field, and the carbon rejection rate per year is as high as more than 90%, so that the carbon fixation capacity of the farmland can be remarkably improved by returning the biochar to the field. However, the existing method for using the biochar is generally to add organic and/or inorganic fertilizers for matching use, so that on one hand, the biochar is troublesome to use and high in cost, and on the other hand, the effect of the biochar is influenced, so that the biochar cannot fully play a role. In addition, the existing biochar has a small microporous structure and a small specific surface area due to the raw materials and the preparation method, and the microporous structure and the specific surface area are one of the factors determining the main functions of the biochar. Moreover, because of the raw materials and the preparation method, the nutrient elements including trace elements reserved by the biochar are less, and the biochar is also one of the reasons that other fertilizers need to be added at present.|[0007] Therefore, the problem to be solved by the technical personnel in the field is how to provide the biochar compound fertilizer which is simple to prepare and convenient to use.|[0008] Disclosure of Invention|[0009] In view of the above, the present invention aims to provide a biochar compound fertilizer, a preparation method and an application thereof, so as to solve the defects in the prior art.|[0010] In order to achieve the purpose, the invention adopts the following technical scheme:|[0011] the biochar compound fertilizer comprises the following raw materials in parts by weight: 50-60 parts of charcoal, 30-40 parts of livestock and poultry manure, 25-35 parts of bamboo powder, 20-30 parts of peanut shell powder, 5-10 parts of binder and 0.8-1.5 parts of composite microbial inoculum;|[0012] preferably: 52-58 parts of charcoal, 32-36 parts of livestock and poultry manure, 28-32 parts of bamboo powder, 22-28 parts of peanut shell powder, 6-9 parts of binder and 0.8-1.2 parts of composite microbial inoculum;|[0013] more preferably: 55 parts of charcoal, 35 parts of livestock and poultry manure, 30 parts of bamboo powder, 25 parts of peanut shell powder, 8 parts of a binder and 1.0 part of a composite microbial inoculum.|[0014] The invention has the advantages that the biochar has the characteristics of looseness, porosity, good air and water permeability, large specific surface area, strong adsorption capacity and chelating capacity, and has the outstanding advantages of safety, environmental protection, high efficiency and the like by being matched with other organic matter raw materials, so that the fertility of organic farmland soil and the carbon sequestration and emission reduction capacity are effectively improved.|[0015] Further, the livestock and poultry manure is at least one of pig manure, cow manure, sheep manure, chicken manure and duck manure.|[0016] The livestock and poultry manure contains rich organic matters, nitrogen, phosphorus, potassium and other nutrients, and can supply various mineral substances and trace elements such as calcium, magnesium, sulfur and the like required by crops, so that the requirements of the crops on various nutrients in the growth process are met.|[0017] Further, the binder is at least one of starch, clay and attapulgite.|[0018] The further technical scheme has the beneficial effects that the binder disclosed by the invention can improve the granulation rate of the fertilizer, and the granule has high strength and is free from agglomeration and moisture regain.|[0019] Further, the composite microbial inoculum is prepared from (2-5) by weight: (1-4): and (1-2) mixing the bacillus subtilis, the actinomycetes and the azomonas.|[0020] The composite microbial inoculum has the beneficial effects that the composite microbial inoculum can fully decompose the biochar, the livestock and poultry manure, the bamboo powder and the peanut shell powder, organic matters generated after fermentation can increase soil gaps, water and air are kept, and nutrient substances are provided for crops.|[0021] A preparation method of a biochar compound fertilizer specifically comprises the following steps:|[0022] (1) weighing the raw materials according to the parts by weight of the biochar compound fertilizer;|[0023] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving to obtain a material A;|[0024] (3) mixing the material A, the livestock and poultry manure and the composite microbial inoculum, and fermenting for 24-36h at 25-35 ℃ to obtain a material B;|[0025] (4) and mixing the material B with a binder, granulating and drying to obtain the biochar compound fertilizer.|[0026] Further, the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2 to 3 hours at the temperature of between 550 and 600 ℃ under the protection of nitrogen, and cooling the plant straws to obtain the plant straw composite material.|[0027] The further technical scheme has the beneficial effects that the preparation condition of the biochar is mild, the biochar is simple and easy to operate, and the prepared biochar has excellent performance.|[0028] Furthermore, in the step (2), the mesh number of the sieved mesh is 100-200 meshes.|[0029] The method has the beneficial effects that the biochar, the bamboo powder and the peanut shell powder are prepared into smaller particles through crushing and sieving, so that the fermentation and granulation drying steps are convenient to carry out.|[0030] In the step (4), the drying temperature is 50-60 ℃, and the drying is carried out until the water content is below 10%.|[0031] The beneficial effect of adopting the further technical scheme is that the biochar compound fertilizer is granulated and dried, and the biochar compound fertilizer absorbs water to expand into powder when being used, so that the contact area of the biochar compound fertilizer and soil is increased, better nutrient absorption of crops is facilitated, and the growth of the crops is promoted.|[0032] The invention also provides application of the biochar compound fertilizer in planting wheat and corn, and the fertilizing amount is 60-80 kg/mu.|[0033] According to the technical scheme, compared with the prior art, the invention has the following beneficial effects:|[0034] the biochar compound fertilizer disclosed by the invention can increase the content of organic matters in soil, improve the structure and porosity of the soil, increase the water and fertilizer storage capacity of the soil, improve the rhizosphere environment of crops, improve the enzyme activity of the soil, promote the reproduction of beneficial microorganisms at the rhizosphere of the crops, make the root system grow robustly and improve the yield of the crops.|INVENTION MODE|[0035] Detailed Description|[0036] The technical solutions in the embodiments of the present invention are clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.|[0037] Example 1|[0038] The biochar compound fertilizer comprises the following raw materials in parts by weight: 50kg of charcoal, 30kg of pig manure, 25kg of bamboo powder, 20kg of peanut shell powder, 5kg of starch, 0.2kg of bacillus subtilis, 0.4kg of actinomycetes and 0.2kg of azomonas;|[0039] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0040] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2 hours at 550 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0041] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture through a 100-mesh sieve to obtain a material A;|[0042] (3) mixing the material A, pig manure, bacillus subtilis, actinomycetes and nitrogen monad, and fermenting for 24 hours at 25 ℃ to obtain a material B;|[0043] (4) and mixing the material B with starch, granulating, and drying at 50 ℃ until the water content is 10% to obtain the biochar compound fertilizer.|[0044] Example 2|[0045] The biochar compound fertilizer comprises the following raw materials in parts by weight: 52kg of charcoal, 32kg of cow dung, 28kg of bamboo powder, 22kg of peanut shell powder, 6kg of clay, 0.2kg of bacillus subtilis, 0.4kg of actinomycetes and 0.2kg of azomonas;|[0046] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0047] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2 hours at 560 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0048] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture through a 120-mesh sieve to obtain a material A;|[0049] (3) mixing the material A, cow dung, bacillus subtilis, actinomycetes and nitrogen monad, and fermenting for 28 hours at 28 ℃ to obtain a material B;|[0050] (4) and mixing the material B with clay, granulating, and drying at 52 ℃ until the water content is 10% to obtain the biochar compound fertilizer.|[0051] Example 3|[0052] The biochar compound fertilizer comprises the following raw materials in parts by weight: 55kg of charcoal, 35kg of chicken manure, 30kg of bamboo powder, 25kg of peanut shell powder, 8kg of clay, 0.5kg of bacillus subtilis, 0.4kg of actinomycetes and 0.1kg of azomonas;|[0053] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0054] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 2.5 hours at 580 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0055] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture through a 150-mesh sieve to obtain a material A;|[0056] (3) mixing the material A, chicken manure, bacillus subtilis, actinomycetes and nitrogen monad, and fermenting for 30 hours at 30 ℃ to obtain a material B;|[0057] (4) and mixing the material B with clay, granulating, and drying at 55 ℃ until the water content is 6% to obtain the biochar compound fertilizer.|[0058] Example 4|[0059] The biochar compound fertilizer comprises the following raw materials in parts by weight: 58kg of charcoal, 36kg of sheep manure, 32kg of bamboo powder, 28kg of peanut shell powder, 9kg of clay, 0.4kg of bacillus subtilis, 0.4kg of actinomycetes and 0.4kg of azomonas;|[0060] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0061] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 3 hours at 580 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0062] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture through a 180-mesh sieve to obtain a material A;|[0063] (3) mixing the material A, sheep manure, bacillus subtilis, actinomycetes and azomonas, and fermenting for 32 hours at 32 ℃ to obtain a material B;|[0064] (4) and mixing the material B with clay, granulating, and drying at 58 ℃ until the water content is 8% to obtain the biochar compound fertilizer.|[0065] Example 5|[0066] The biochar compound fertilizer comprises the following raw materials in parts by weight: 60kg of charcoal, 40kg of duck manure, 35kg of bamboo powder, 30kg of peanut shell powder, 10kg of attapulgite, 0.6kg of bacillus subtilis, 0.6kg of actinomycetes and 0.3kg of azomonas;|[0067] the preparation method of the biochar compound fertilizer specifically comprises the following steps:|[0068] (1) weighing the raw materials according to the weight of the biochar compound fertilizer; the preparation method of the biochar comprises the following steps: crushing plant straws, putting the crushed plant straws into a carbonization furnace, pyrolyzing the crushed plant straws for 3 hours at 600 ℃ under the protection of nitrogen, and cooling the crushed plant straws to obtain the plant straws;|[0069] (2) mixing and crushing the biochar, the bamboo powder and the peanut shell powder, and sieving the mixture by a 200-mesh sieve to obtain a material A;|[0070] (3) mixing the material A, duck manure, bacillus subtilis, actinomycetes and azomonas, and fermenting at 35 ℃ for 36 hours to obtain a material B;|[0071] (4) and mixing the material B and the attapulgite, granulating, and drying at 60 ℃ until the water content is 8% to obtain the biochar compound fertilizer.|[0072] Performance testing|[0073] 1. The biochar compound fertilizers prepared in the embodiments 1 to 5 are respectively taken and tested for effective viable count, organic matter, moisture, pH value, fecal coliform count and ascarid egg death rate according to the test method and requirements of NYT 3618-2020 biochar-based organic fertilizer.|[0074] The measurement results are shown in table 1.|[0075] Table 1 examples 1-3 results of measuring properties of biofertilizers|[0076] |[0077] As can be seen from Table 1, all indexes of the biochar compound fertilizer prepared by the embodiments 1-5 of the invention all meet the corresponding requirements of NYT 3618-2020 biochar-based organic fertilizer. Among them, example 3 is the most preferable example.|[0078] 2. Corn field test|[0079] Selecting a corn test field in Zhengzhou city in Henan province, averagely dividing the corn test field into two parts, recording the two parts as a conventional fertilization area and a test fertilization area, selecting Zhonghe 107 corn varieties, respectively counting the grain number of each ear, the thousand grain weight and the yield of the corn after the corn is mature, and calculating the yield increasing rate.|[0080] The specific fertilization method of the conventional fertilization area comprises the following steps: local conventional fertilization, namely respectively applying base fertilizer, seedling-slow fertilizer, tiller fertilizer and spike fertilizer for 4 times by adopting a stage fertilization method, wherein the fertilization amount and the fertilization mode are consistent with those of local agricultural production; the specific fertilization method of the experimental fertilization area comprises the following steps: 80kg of the biochar compound fertilizer prepared in the embodiment 3 is applied to each mu of land at one time in a base fertilizer mode, and other fertilizers are not applied additionally.|[0081] The statistical results are shown in table 2.|[0082] TABLE 2 statistics of maize in conventional and experimental fertilization zones|[0083] Measurement indexGrain number of spike (grain)Thousand Kernel weight (g)Yield (kg/mu)Conventional fertilization area481235.12445.63Experimental fertilization district584276.58536.88Yield increase (%)21.4117.6320.48|[0084] As can be seen from Table 2, the grain number per ear, the thousand grain weight and the yield of the corns in the experimental fertilization area are all superior to those in the conventional fertilization area, wherein the grain number per ear is increased by 21.41%, the thousand grain weight is increased by 17.63%, and the yield is increased by 20.48%.|[0085] The tests show that the biochar compound fertilizer can increase the content of organic matters in soil, improve the structure and porosity of the soil, increase the water and fertilizer storage capacity of the soil, improve the rhizosphere environment of crops, improve the enzyme activity of the soil, promote the multiplication of beneficial microorganisms in the rhizosphere of the crops, make the root systems grow healthily and improve the yield of the crops.|[0086] The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. Family Number|(92088576)|92088576|Abstract|(CN112142537 A)|The invention discloses a biochar compound fertilizer which comprises the following raw materials in parts by weight : 50-60 parts of biochar , 30-40 parts of livestock and poultry manure , 25-35 parts of bamboo powder , 20-30 parts of peanut shell powder , 5-10 parts of a binder and 0.8-1.5 parts of a complex microbial inoculant . The preparation method comprises the following steps : ( 1 ) weighing the raw materials ; ( 2 ) mixing , crushing and sieving the biochar , the bamboo powder and the peanut shell powder ; ( 3 ) mixing with livestock and poultry manure and the complex microbial inoculant , and fermenting ; and ( 4 ) mixing with the binder , granulating and drying to obtain the biochar compound fertilizer . The biochar has the characteristics of being loose , porous , good in air permeability and water permeability , large in specific surface area and high in adsorption capacity and chelating capacity , and has the outstanding advantages of being safe , environmentally friendly , efficient and the like incooperation with other organic raw materials , and therefore the organic farmland soil fertility and the carbon sequestration and emission reduction capacity are effectively improved . |CPC codes|(CN112142537 A)|A01C - 021/00 |IPC codes|(CN112142537 A)|A01C - 021/00 | Basic materials chemistry|Other special machines A01C-021/00|C05D-009/00|C05F-017/20|C05G-003/00|C05G-003/80|C05G-005/12|Y02W-030/40 (GR1) C05D-009/00[RK1]; C05F-003/00[RK2]; C05F-005/00/2[RK3]; C05F-011/00[RK4]; C05G-003/00[RK5]; C05G-003/80[RK6]; C05G-005/12[RK7] A01C-021/00|C05D-009/00|C05F-017/20|C05G-003/00|C05G-003/80|C05G-005/12|Y02W-030/40 A01C-021/00|C05F-017/20|C05G-003/00|C05G-003/80|C05G-005/12 A01C-021/00|C05F-017/20|C05G-003/00|C05G-003/80|C05G-005/12 CN113664032|CN113636895 CN113664032 97109523 WHO=Examiner SELF=N CAT=A|CN113636895 96987418 WHO=Examiner SELF=N CAT=A CN103833445|CN103396171|CN109879709|CN106242734|CN104072303|CN103626610 CN103833445 66162085 WHO=Examiner SELF=N CAT=Y CAT=X|CN103396171 59347130 WHO=Examiner SELF=N CAT=Y|CN109879709 84876679 WHO=Examiner SELF=N CAT=A|CN106242734 74949005 WHO=Examiner SELF=N CAT=A|CN104072303 67547721 WHO=Examiner SELF=N CAT=A|CN103626610 64940398 WHO=Examiner SELF=N CAT=A 张运红等: &quot;土壤改良剂对镉污染土壤小麦抗性、&quot;, 《河南农业科学》 (Cat. A) CN103396171; CN103626610; CN103833445; CN104072303; CN106242734; CN109879709 REVOKED (CN112142537)|REVOKED DEAD (CN112142537)|DEAD (CN112142537)|LEGAL DETAILS FOR CN112142537|Actual or expected expiration date=2022-12-23|Legal state=DEAD|Status=REVOKED|Event publication date=2020-11-09|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202011240804|Application date=2020-11-09|Standardized application number=2020CN-1240804|Event publication date=2020-12-29|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN112142537|Publication stage code=A|Publication date=2020-12-29|Standardized publication number=CN112142537|Event publication date=2020-12-29|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2021-01-15|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2022-12-23|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRHYytYm0r5rlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000055264819&ekey=1901&xpn=CN112142537&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=qHuFvRkujZsXsQ39MbsEjJNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN112142537)|CN (CN112142537)|NAME=INSTITUTE OF PLANT NUTITUION AND RESOURCE ENVIRONMENT, HENAN ACADEMY OF AGRICULTURAL SCIENCES , COUNTRY=CN (CN112142537)|NAME=ZHAO XUPING;MUDA INTELLECTUAL PROPERTY , REG=11465 (CN112142537)|NAME=DU JUN|NAME=YANG HUANHUAN|NAME=HU YING|NAME=HE AILING|NAME=PAN XIUYAN|NAME=XU JIDONG|NAME=LIU GAOYUAN 0 1 Titre: (CN112142537)|Biochar compound fertilizer as well as preparation method and application thereof Résumé: (CN112142537)|The invention discloses a biochar compound fertilizer which comprises the following raw materials in parts by weight: 50-60 parts of biochar, 30-40 parts of livestock and poultry manure, 25-35 parts of bamboo powder, 20-30 parts of peanut shell powder, 5-10 parts of a binder and 0.8-1.5 parts of a complex microbial inoculant. The preparation method comprises the following steps: (1) weighing the raw materials; (2) mixing, crushing and sieving the biochar, the bamboo powder and the peanut shell powder; (3) mixing with livestock and poultry manure and the complex microbial inoculant, and fermenting; and (4) mixing with the binder, granulating and drying to obtain the biochar compound fertilizer. The biochar has the characteristics of being loose, porous, good in air permeability and water permeability, large in specific surface area and high in adsorption capacity and chelating capacity, and has the outstanding advantages of being safe, environmentally friendly, efficient and the like incooperation with other organic raw materials, and therefore the organic farmland soil fertility and the carbon sequestration and emission reduction capacity are effectively improved. 84 Abstract gpt-4o-mini no The article focuses on biochar as a fertilizer and its preparation method, without a central emphasis on accelerated weathering or CO₂ capture through mineral alteration.
84 CN202410643788 CN202410643788 CN118603924 111335901 CN118603924 A 2024-09-06 [CN118603924] 2024-05-23 2024-05-23 2024-09-06 (CN118603924)|2044-05-23 (CN118603924)|Method for measuring fixed carbon dioxide content of silicate product (CN118603924)|The invention provides a method for determining the fixed carbon dioxide content of a silicate product, which comprises the following steps: S1, sampling two groups of test blocks before and after carbon maintenance, drying, crushing and grinding to below 200 meshes; s2, crucible pretreatment: carrying out heat preservation on the crucible at 800-1400 DEG C for 1-4 hours, and storing the crucible in a dryer; s3, detecting by an infrared carbon-sulfur analyzer: weighing the sample prepared in the step S1, putting the sample into the crucible pretreated in the step S2, uniformly covering the crucible with a fluxing agent, and analyzing on the infrared carbon-sulfur analyzer; s4, calculating the carbon sequestration amount, wherein the ratio of the carbon content difference value before and after carbon maintenance to the sample mass is the carbon sequestration amount. SHANGHAI JIANYAN BUILDING MATERIAL TECHNOLOGY|SHANGHAI RESEARCH INSTITUTE OF BUILDING SCIENCES (CN118603924)|SHANGHAI RESEARCH INSTITUTE OF BUILDING SCIENCES CO., LTD ([CN])|SHANGHAI JIANYAN BUILDING MATERIAL TECH CO LTD LIN MAOSONG|YANG GUANG|YANG LIXIANG|WANG QIONG (CN118603924)|LIN MAOSONG|YANG GUANG|YANG LIXIANG|WANG QIONG (CN118603924)|CAI JIAJIE;SHANGHAI JIUZE LAWYER AFFAIRS|Reg. Nb: 31337 (CN118603924)|This process is also very error-prone, since silicate products are complex mixtures, and other hydration product components slowly decompose during 500-850 ℃ to cause mass loss; meanwhile, the method cannot distinguish whether the calcium carbonate is self-contained in the raw material or generated during the carbon fixation maintenance.| (CN118603924)|1. A method for determining the fixed carbon dioxide content of a silicate article comprising the steps of: s1, sampling two groups of test blocks before and after carbon maintenance, respectively drying, crushing, grinding and sieving; to below 200 meshes; S2, crucible pretreatment: preserving the crucible at 800-1400 ℃ for 1-4 hours, and placing the crucible in a dryer for preservation; s3, detecting by an infrared carbon-sulfur analyzer: Weighing the sample prepared in the step S1, putting the sample into the crucible pretreated in the step S2, uniformly covering a fluxing agent on the crucible, and analyzing the sample on an infrared carbon-sulfur analyzer; S4, calculating the carbon sequestration amount: the difference of the carbon content before and after the carbon maintenance/the mass of the sample is the carbon fixation amount. | (CN118603924)|The invention provides a method for determining the fixed carbon dioxide content of silicate products, which comprises the following steps: s1, sampling two groups of test blocks before and after carbon maintenance, and crushing and grinding the test blocks to below 200 meshes after drying; s2, crucible pretreatment: preserving the crucible at 800-1400 ℃ for 1-4 hours, and placing the crucible in a dryer for preservation; s3, detecting by an infrared carbon-sulfur analyzer: weighing the sample prepared in the step S1, putting the sample into the crucible pretreated in the step S2, uniformly covering a fluxing agent on the crucible, and analyzing the sample on an infrared carbon-sulfur analyzer; s4, calculating the carbon sequestration amount: the difference of the carbon content before and after the carbon maintenance/the mass of the sample is the carbon fixation amount.|The invention provides a method for measuring the fixed carbon dioxide content of silicate products by using an infrared carbon-sulfur analyzer, wherein the infrared carbon-sulfur analyzer used in the method is a full-automatic analyzer for analyzing the carbon and sulfur content in metals, ores, soil and other substances in the industries of metallurgy, machinery, chemical industry and the like, but the application of the infrared carbon-sulfur analyzer in the detection of the carbon content in silicate products is not seen at present.| (CN118603924)|CARBON DIOXIDE(100,28)|SILICATE PRODUCT(100,28)|CARBON DIOXIDE CONTENT(100,24)|INFRARED CARBON SULFUR ANALYZER(100,23)|SILICATE ARTICLE(100,3)|MEASURING(100,1)|CRUCIBLE PRETREATMENT(75,8)|CRUCIBLE(73,25)|CARBON MAINTENANCE(48,3)|CRUSHING(39,3)|CARBON CONTENT(38,23)|CARBON CONTENT DIFFERENCE(37,3)|CARBON ANALYZER(36,1)|PRESERVATION(35,7)|SULFUR CONTENT(33,1)|CARBON FIXATION(31,57)|HYDRATION PRODUCT COMPONENT(28,1)|DRYER(27,7)|CARBON SEQUESTRATION(25,7)|FULL AUTOMATIC ANALYZER(25,1)|MACHINERY(25,1)|TEST BLOCK(24,19)|TUNGSTEN PARTICLE(24,3)|CARBON CURING(24,1)|CARBON FIXATION MAINTENANCE(23,21)|QUARTERING(23,12)|FLUXING AGENT(22,11)|SIEVING(21,4)|TIN PARTICLE(21,3)|CARBON FIXING CURING(20,1)|ORE(20,1)|ERROR PRONE(19,1)|GROUND(19,1)|MASS LOSS(18,2)|GRINDING(16,9)|CALCIUM CARBONATE(15,2)|DRYING CONDITION(15,2)|CHEMICAL INDUSTRY(13,1)|PRETREATED CRUCIBLE(12,2)|PSI(11,6)|COMPLEX MIXTURE(11,1)|SQUARE HOLE SIEVE(10,5)|COMPARISON LEVEL(9,3)|SAMPLE PRETREATMENT(8,9)|CONCRETE SAMPLE CARBON CONTENT(8,3)|CONSTANT WEIGHT(8,2)|SATURATED HUMIDITY(8,2)|CEMENT HYDRATION(8,1)|FIXED CARBON CONTENT(8,1)|THERMOGRAVIMETRIC ANALYZER(8,1)|OVEN(7,9)|CARBON FIXATION CALCULATION(7,4)|MOISTURE CORRECTING ERROR(7,1)|CEMENT BOARD SAMPLE(6,3)|CEMENT BOARD BATCH(6,2)|INFRARED SULFUR CARBON ANALYZER(6,2)|INSPECTION(6,2)|QUANTITATIVE DETECTION(6,2)|SYMMETRICAL SAMPLE(6,2)|CRUCIBLE PRETREATMENT TEMPERATURE(6,1)|FLUX CHOICE(6,1)|INSUFFICIENT SAMPLE COMBUSTION(6,1)|REDUNDANT DUST(6,1)|CARRIER GAS PRESSURE(5,3)|DYNAMIC AIR PRESSURE(5,3)|AUTOCLAVED AERATED CONCRETE BLOCK(5,2)|CARBON FIXING MAINTENANCE(5,2)|CONCRETE TEST BLOCK BATCH(5,2)|HCS 500 INFRARED CARBON(5,2)|RAW MATERIAL(5,2)|ANALYSIS TIME(4,3)|SAMPLING BLOCK(4,3)|CALCIUM CARBONATE DECOMPOSITION(4,1)|ERROR CORRECTION(4,1)|INCOMPLETE CARBON RELEASE(4,1)|MACROSCOPIC QUALITY DIFFERENCE(4,1)|ORDINARY SKILL PERSON(4,1)|REPEAT ABILITY(4,1)|STOP HYDRATION(4,1)|TECHNICAL BOTTLE(4,1)|ABSOLUTE DRY QUALITY(3,1)|CARBON FIXATION POTENTIAL(3,1)|CARBON SEQUESTRATION PERFORMANCE(3,1)| (CN118603924)|1. A method for determining the fixed carbon dioxide content of a silicate article comprising the steps of:| s1, sampling two groups of test blocks before and after carbon maintenance, respectively drying, crushing, grinding and sieving; to below 200 meshes; | S2, crucible pretreatment: | preserving the crucible at 800-1400 ℃ for 1-4 hours, and placing the crucible in a dryer for preservation; | s3, detecting by an infrared carbon-sulfur analyzer: | Weighing the sample prepared in the step S1, putting the sample into the crucible pretreated in the step S2, uniformly covering a fluxing agent on the crucible, and analyzing the sample on an infrared carbon-sulfur analyzer; | S4, calculating the carbon sequestration amount: | the difference of the carbon content before and after the carbon maintenance/the mass of the sample is the carbon fixation amount. |2. The method for determining the fixed carbon dioxide content of a silicate product according to claim 1, wherein the drying condition in step S1 is 105 ℃ to constant weight.|3. The method for determining the fixed carbon dioxide content of a silicate product according to claim 1, wherein the front and rear sets of test blocks in step S1 are taken from the same batch of test blocks before and after the carbon fixing curing, respectively.|4. The method for measuring the fixed carbon dioxide content of a silicate product according to claim 1, wherein in step S3, the samples before and after the carbon curing are weighed in equal amounts, and the flux is uniformly covered with 1 to 3g for each 0.1 to 0.5g of the samples for both groups of samples.|5. A method for determining the fixed carbon dioxide content of a silicate product according to claim 1 or 3, wherein in step S1, the sample is broken into particles of less than 10mm, sampled by a quartering method, and ground and sieved.|6. The method for determining the fixed carbon dioxide content of a silicate product according to claim 1, wherein in step S4, the fixed carbon content is calculated using the following formula:| wherein, C: silicate product fixes carbon dioxide content% |C2: carbon content of sample after carbon fixation%|C1: carbon content of the sample before carbon fixation,%.|7. The method for measuring the fixed carbon dioxide content of a silicate product according to claim 1, wherein the flux in the step S3 is one or a mixture of more than two of tungsten particles, tin particles and pure iron.|8. The method for determining the fixed carbon dioxide content of a silicate product according to claim 1, wherein the infrared carbon sulfur analyzer is an HCS-500 infrared carbon sulfur analyzer.|9. The method for determining the fixed carbon dioxide content of a silicate article according to claim 1 or 8, wherein the operating conditions of the infrared carbon sulfur analyzer are: carrier flow rate is 2-4L/min, carrier gas pressure is 30-40 psi, and dynamic air pressure is 35-45 psi.|10. The method for measuring the fixed carbon dioxide content of a silicate product according to claim 9, wherein in step S3, the analysis time is 30 to 50S and the comparison level is 2 to 4. (CN118603924)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of physical and chemical inspection, and particularly relates to a method for measuring the content of fixed carbon dioxide in silicate products by using an infrared sulfur-carbon analyzer.|BACKGROUND ART|[0002] The products such as calcium hydroxide, hydrated calcium silicate and the like generated in the cement hydration process of silicate products can react with carbon dioxide to be converted into carbonate, so that the stable sealing and storage of greenhouse gases are realized, and the silicate products have higher carbon fixation potential. The carbon sequestration amount is an important index for evaluating the carbon sequestration performance, economy and environmental benefit of materials, and the common detection methods include the following types, but all have technical bottlenecks, and the carbon sequestration amount cannot be accurately determined:|[0003] 1) Macroscopic quality difference method |[0004] And detecting the mass of the test block before and after the carbon fixation maintenance by adopting a manual weighing method, and representing the carbon fixation amount by using the mass difference of the test block and the test block. The method omits evaporation of water during the curing of the carbon fixation, and causes larger error of test results. There are studies on correcting errors of moisture by means of absolute dry quality, evaporated water compensation, saturated humidity and the like, but because moisture continuously participates in hydration reaction to produce solid substances during carbon fixation, a certain amount of moisture is still maintained in hydration products in an absolute dry state after carbon fixation maintenance, and the errors are unavoidable; on the other hand, the water can dissolve part of carbon dioxide, and new errors can be brought by evaporating water or saturated humidity.|[0005] 2) Microscopic analysis method|[0006] And analyzing the sample of the test block after the carbon fixation maintenance by adopting a thermogravimetric analyzer, and representing the carbon fixation amount by using the mass loss of calcium carbonate decomposition at about 500-850 ℃. This process is also very error-prone, since silicate products are complex mixtures, and other hydration product components slowly decompose during 500-850 ℃ to cause mass loss; meanwhile, the method cannot distinguish whether the calcium carbonate is self-contained in the raw material or generated during the carbon fixation maintenance.|DISCLOSURE|Disclosure of Invention|[0007] The invention aims to solve the technical problems of large error and poor accuracy of the existing detection method, and provides a method for detecting the carbon dioxide content of silicate products by utilizing an infrared sulfur-carbon analyzer, which can realize quantitative detection of the carbon fixation amount of silicate products and has high accuracy and high reliability of detection results,|[0008] The technical problems to be solved by the method can be implemented by the following technical schemes.|[0009] A method for determining the fixed carbon dioxide content of a silicate product, comprising the steps of:|[0010] S1, sampling two groups of test blocks before and after carbon maintenance, respectively drying, crushing, grinding and sieving; to below 200 meshes; wherein 200 mesh is the expected grinding value (sample is expected to be no greater than 200 mesh, where 200 mesh is the expected value); during sieving, a square hole sieve with 0.04-0.08mm can be selected; |[0011] S2, crucible pretreatment: |[0012] the crucible is kept at 800-1400 ℃ for 1-4 h and is put into a dryer for preservation |[0013] S3, detecting by an infrared carbon-sulfur analyzer:|[0014] Weighing the sample prepared in the step S1, putting the sample into the crucible pretreated in the step S2, uniformly covering a fluxing agent on the crucible, and analyzing the sample on an infrared carbon-sulfur analyzer; |[0015] S4, calculating the carbon sequestration amount: |[0016] the difference of the carbon content before and after the carbon maintenance/the mass of the sample is the carbon fixation amount. |[0017] Further, the drying condition in step S1 is 105 ℃ to constant weight.|[0018] Further, the front and rear groups of test blocks in the step S1 are respectively taken from a batch of test blocks before and after the carbon fixing maintenance.|[0019] Preferably, in step S3, 1-3g of flux is uniformly covered every 0.1-0.5g of sample during weighing. Each sample was weighed and tested separately, and the two samples obtained were weighed in equal amounts before and after carbon fixation.|[0020] Further, in the step S1, after the sample is crushed to particles with the particle diameter of less than 10mm, sampling is carried out by a quartering method, and then grinding and sieving are carried out.|[0021] Further, in step S4, the carbon sequestration amount is calculated using the following formula:|[0022] |[0023] wherein, C: silicate product fixes carbon dioxide content% |[0024] C2: carbon content of sample after carbon fixation%|[0025] C1: carbon content of the sample before carbon fixation,%.|[0026] Further, the fluxing agent in the step S3 is one or a mixture of more than two of tungsten particles, tin particles and pure iron.|[0027] Preferably, the infrared carbon and sulfur analyzer is an HCS-500 infrared carbon and sulfur analyzer.|[0028] Preferably, the working conditions of the infrared carbon sulfur analyzer are as follows: carrier flow rate is 2-4L/min, carrier gas pressure is 30-40 psi, and dynamic air pressure is 35-45 psi.|[0029] Preferably, in step S3, the analysis time is 30 to 50 seconds, and the comparison level is 2 to 4.|[0030] Compared with the prior art, the invention has the following beneficial effects:|[0031] (1) The sample detected by the method is a test block before and after carbon fixation maintenance of the same batch of products, and is scientifically sampled by full crushing and a quartering method, and the sample is representative and can accurately reflect the carbon fixation amount in the carbon maintenance process. |[0032] (2) The sample pretreatment method provided by the invention adopts 105 ℃ drying to remove moisture and stop hydration, so that errors caused by the fact that products are continuously hydrated to generate new solid products are avoided; and the sealed air-insulated storage is adopted to avoid errors caused by carbon dioxide contact, and the device has the characteristic of high accuracy.|[0033] (3) The detection method provided by the invention has reliable results and high repeatability, and is suitable for the determination of solid carbon content of various silicate products.|INVENTION MODE|Detailed Description|[0034] The following detailed description of specific embodiments of the invention is provided in further detail.|[0035] The invention provides a method for measuring the fixed carbon dioxide content of silicate products by using an infrared carbon-sulfur analyzer, wherein the infrared carbon-sulfur analyzer used in the method is a full-automatic analyzer for analyzing the carbon and sulfur content in metals, ores, soil and other substances in the industries of metallurgy, machinery, chemical industry and the like, but the application of the infrared carbon-sulfur analyzer in the detection of the carbon content in silicate products is not seen at present. And because the raw materials of silicate products often have implicit carbon components, the carbon fixation amount cannot be represented by directly using the carbon content result of the test block after carbon fixation maintenance.|[0036] The following steps of the method are as follows:|[0037] (1) Pretreatment of a sample before carbon fixation: |[0038] randomly extracting 1-3 test blocks into 1 group in the same batch of test blocks before carbon fixation maintenance, immediately drying in a 105 ℃ oven until the weight is constant, respectively crushing each test block to 0-10mm particles, respectively sampling 25-100g of samples by a quartering method, grinding the samples, sieving with a 0.04-0.08mm square hole sieve, and sealing for later use; |[0039] (2) Sample pretreatment after carbon fixation maintenance: |[0040] randomly extracting 1-3 test blocks into 1 group from the same batch of test blocks after the carbon fixation maintenance is finished, immediately drying in a 105 ℃ oven until the weight is constant, respectively crushing all the test blocks to 0-10mm particles, respectively sampling 25-100g of samples by a quartering method, grinding the samples, sieving the samples by a square hole sieve of 0.04-0.08mm, and sealing for later use; |[0041] (3) Crucible pretreatment: |[0042] preserving the crucible at 800-1400 ℃ for 1-4 hours, and placing the crucible in a dryer for preservation; |[0043] (4) And (3) detecting by an infrared carbon-sulfur analyzer: |[0044] Weighing 0.1-0.5g of sample before and after curing of carbon fixation, placing the sample into a pretreated crucible, uniformly covering 1-3g of fluxing agent on the crucible, and analyzing the sample on an infrared carbon-sulfur analyzer. |[0045] (5) Calculation of carbon fixation: the formula for calculating the carbon fixation is as follows:|[0046] |[0047] wherein, C: silicate product fixes carbon dioxide content% |[0048] C2: carbon content of sample after carbon fixation%|[0049] C1: carbon content of sample before carbon fixation%|[0050] The average value of the fixed carbon dioxide content of 3 test pieces is taken as a final test result, and the test result is repaired to be about 2 bits after decimal places.|[0051] In the steps (1) and (2), 3 test blocks are randomly extracted from the same batch of test blocks after the carbon fixation maintenance is finished to form 1 group, the test blocks are immediately dried in a 105 ℃ oven until the weight is constant, each test block is respectively crushed to 0-10mm particles, 50-60g of samples are respectively sampled by a quartering method, and the samples are ground and then are sealed for later use after being screened by a square hole sieve of 0.04-0.08 mm;|[0052] Preferably, the temperature of the crucible pretreatment in the step (3) is 1000-1200 ℃, and the temperature is kept for 2-3 hours. |[0053] Preferably, in the step (4), the sample is weighed in an amount of 0.2 to 0.3g.|[0054] The fluxing agent in the step (4) is one or a mixture of more than two of tungsten particles, tin particles and pure iron. The flux is preferably weighed in an amount of 2-3g.|[0055] The infrared carbon and sulfur analyzer in the step (4) is preferably an HCS-500 infrared carbon and sulfur analyzer.|[0056] The working conditions of the infrared carbon-sulfur analyzer in the step (4) are as follows: carrier flow rate is 2-4L/min, carrier gas pressure is 30-40 psi, and dynamic air pressure is 35-45 psi.|[0057] The analysis time in the step (4) is 30-50 s, and the comparison level is 2-4.|[0058] The determination method provided by the invention solves the problems that the method for detecting the carbon content of silicate products is inaccurate and the requirement of quantitative detection cannot be met.|[0059] The method of determining the fixed carbon dioxide content of silicate articles of the present invention is further illustrated below in conjunction with specific examples, which are provided to illustrate the invention and are not intended to limit the scope of the invention.|[0060] Example 1|[0061] The method for determining the fixed carbon dioxide content of the silicate product provided by the embodiment mainly comprises the following steps:|[0062] (1) Pretreatment of a sample before carbon fixation: |[0063] Randomly extracting 3 test blocks into 1 group from the same batch of concrete test blocks before carbon fixation maintenance, immediately drying in a 105 ℃ oven until the weight is constant, crushing all the test blocks into particles below 10mm, respectively sampling 50g of samples by a quartering method, grinding, sieving with a 0.08mm square hole sieve, and sealing for later use; |[0064] (2) Sample pretreatment after carbon fixation maintenance: |[0065] Randomly extracting 3 test blocks into 1 group from the same batch of concrete test blocks after the carbon fixation maintenance is finished, immediately drying in a 105 ℃ oven until the weight is constant, crushing all the test blocks into particles below 10mm, respectively sampling 50g of samples by a quartering method, grinding, sieving by a square hole sieve of 0.08mm, and sealing for later use; |[0066] (3) Crucible pretreatment: |[0067] preserving the crucible at 1200 ℃ for 2 hours, and placing the crucible in a dryer for preservation; |[0068] (4) And (3) detecting by an infrared carbon-sulfur analyzer: |[0069] Weighing 0.2g of samples before and after carbon fixation maintenance, putting the samples into a crucible after pretreatment, uniformly covering 2g of fluxing agent on the samples, and analyzing the samples on an infrared carbon-sulfur analyzer; |[0070] (5) Calculation of carbon fixation: |[0071] The carbon content of the concrete sample before carbon fixation is 2.23%, 2.25% and 2.26%, and the carbon content of the concrete sample after carbon fixation is 2.58%, 2.59% and 2.56%, and the carbon content of the concrete sample after carbon fixation is 1.21% according to the formula. |[0072] Example 2|[0073] The method for determining the fixed carbon dioxide content of the silicate product provided by the embodiment mainly comprises the following steps:|[0074] (1) Pretreatment of a sample before carbon fixation: |[0075] randomly extracting 3 test blocks into 1 group in the same batch of autoclaved aerated concrete blocks before carbon fixing maintenance, immediately drying in a 105 ℃ oven until the weight is constant, crushing all the test blocks into particles below 5mm, respectively sampling 50g of samples by a quartering method, grinding, sieving with a 0.08mm square hole sieve, and sealing for later use; |[0076] (2) Sample pretreatment after carbon fixation maintenance: |[0077] Randomly extracting 3 test blocks into 1 group in the same batch of autoclaved aerated concrete blocks after the carbon fixation maintenance is finished, immediately drying in a 105 ℃ oven until the weight is constant, crushing all the test blocks into particles below 5mm, respectively sampling 50g of samples by a quartering method, grinding, sieving by a square hole sieve of 0.08mm, and sealing for later use; |[0078] (3) Crucible pretreatment: |[0079] preserving the crucible at 1000 ℃ for 3 hours, and placing the crucible in a dryer for preservation; |[0080] (4) And (3) detecting by an infrared carbon-sulfur analyzer: |[0081] Weighing 0.3g of samples before and after carbon fixation maintenance, putting the samples into a crucible after pretreatment, uniformly covering 2.5g of fluxing agent on the samples, and analyzing the samples on an infrared carbon-sulfur analyzer; |[0082] (5) Calculation of carbon fixation: |[0083] the carbon content of the autoclaved aerated concrete block sample before carbon fixation is 0.83%, 0.84% and 0.83%, and the carbon content of the autoclaved aerated concrete block sample after carbon fixation is 1.02%, 1.03% and 10.4%, and the fixed carbon dioxide content of the autoclaved aerated concrete block sample is calculated to be 0.72% according to a formula. |[0084] Example 3|[0085] The method for determining the fixed carbon dioxide content of the silicate product provided by the embodiment mainly comprises the following steps:|[0086] (1) Pretreatment of a sample before carbon fixation: |[0087] Randomly extracting 3 test blocks into 1 group in the same batch of cement boards before carbon fixation maintenance, immediately drying in a 105 ℃ oven until the weight is constant, completely crushing each test block into particles below 5mm, respectively sampling 60g of samples by a quartering method, grinding, sieving with a 0.04mm square hole sieve, and sealing for later use; |[0088] (2) Sample pretreatment after carbon fixation maintenance: |[0089] Randomly extracting 3 test blocks into 1 group from the same batch of cement boards after the carbon fixation maintenance is finished, immediately drying in a 105 ℃ oven until the weight is constant, completely crushing each test block into particles below 5mm, respectively sampling 60g of samples by a quartering method, grinding, sieving by a 0.04mm square hole sieve, and sealing for later use; |[0090] (3) Crucible pretreatment: |[0091] preserving the crucible at 1200 ℃ for 2 hours, and placing the crucible in a dryer for preservation; |[0092] (4) And (3) detecting by an infrared carbon-sulfur analyzer: weighing 0.2g of samples before and after carbon fixation maintenance, putting the samples into a pretreated crucible, uniformly covering 2g of fluxing agent on the samples, and analyzing the samples on an infrared carbon-sulfur analyzer. |[0093] (5) Calculation of carbon fixation: the carbon content of the cement board sample before carbon fixation is 4.21%, 4.19% and 4.22%, the carbon content of the cement board sample after carbon fixation is 5.12%, 5.13% and 5.13%, and the carbon content of the cement board sample after carbon fixation is 3.39% according to the formula.|[0094] Example 4 (non-preferred operation)|[0095] The selection of the sample weighing has a certain influence on the accuracy of analysis results. Too low a sample weight may result in a low sample representation, and too high a sample weight may result in incomplete carbon release from the sample and may result in a lower analysis result. The symmetrical sample amounts were tested using a standard sample having a carbon content of 1.00%.|[0096] The experimental process comprises the following steps: weighing 0.1-0.5 g of standard sample, placing the standard sample into a crucible pretreated for 2 hours at 1200 ℃, uniformly covering 2g of fluxing agent on the crucible, and analyzing the mixture on an infrared carbon-sulfur analyzer.|[0097] TABLE 1 influence of Standard sample Scale on detection results|[0098] Standard sample weighing gDetection value%Detection value%Detection value%Average%0.10.970.980.950.970.20.9811.000.990.30.9911.001.000.40.960.960.950.960.50.960.940.950.95|[0099] The sample amount is preferably 0.2 to 0.3g by comparison of the average value in table 1 and the carbon content of the standard sample.|[0100] Example 5 (non-preferred operation)|[0101] The choice of flux weighing also has a certain impact on the accuracy of the analysis results. The too low flux weighing amount can lead to insufficient sample combustion and lower analysis result; the flux is excessively high in sample weighing amount, so that the sample is easy to splash and redundant dust is easy to generate, and the analysis result is influenced. The symmetrical sample amounts were tested using a standard sample having a carbon content of 1.00%.|[0102] The experimental process comprises the following steps: 0.2g of standard sample is weighed, placed in a crucible pretreated for 2 hours at 1200 ℃, evenly covered with 1-5 g of fluxing agent, and analyzed on an infrared carbon-sulfur analyzer.|[0103] TABLE 2 influence of flux sample weights on detection results|[0104] Flux weighing gDetection value%Detection value%Detection value%Average%1.00.940.950.950.952.00.980.991.000.993.01.000.991.001.004.00.940.950.940.945.00.930.940.930.93|[0105] The sample amount is preferably 2 to 3g by comparison of the average value in table 2 and the carbon content of the standard sample.|[0106] The previous description of the embodiments is provided to facilitate a person of ordinary skill in the art in order to make and use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments, and those skilled in the art, based on the principle of the present invention, should make improvements and modifications without departing from the scope of the present invention. (CN118603924)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of physical and chemical inspection, and particularly relates to a method for measuring the content of fixed carbon dioxide in silicate products by using an infrared sulfur-carbon analyzer.|BACKGROUND ART|[0002] The products such as calcium hydroxide, hydrated calcium silicate and the like generated in the cement hydration process of silicate products can react with carbon dioxide to be converted into carbonate, so that the stable sealing and storage of greenhouse gases are realized, and the silicate products have higher carbon fixation potential. The carbon sequestration amount is an important index for evaluating the carbon sequestration performance, economy and environmental benefit of materials, and the common detection methods include the following types, but all have technical bottlenecks, and the carbon sequestration amount cannot be accurately determined:|[0003] 1) Macroscopic quality difference method |[0004] And detecting the mass of the test block before and after the carbon fixation maintenance by adopting a manual weighing method, and representing the carbon fixation amount by using the mass difference of the test block and the test block. The method omits evaporation of water during the curing of the carbon fixation, and causes larger error of test results. There are studies on correcting errors of moisture by means of absolute dry quality, evaporated water compensation, saturated humidity and the like, but because moisture continuously participates in hydration reaction to produce solid substances during carbon fixation, a certain amount of moisture is still maintained in hydration products in an absolute dry state after carbon fixation maintenance, and the errors are unavoidable; on the other hand, the water can dissolve part of carbon dioxide, and new errors can be brought by evaporating water or saturated humidity.|[0005] 2) Microscopic analysis method|[0006] And analyzing the sample of the test block after the carbon fixation maintenance by adopting a thermogravimetric analyzer, and representing the carbon fixation amount by using the mass loss of calcium carbonate decomposition at about 500-850 ℃. This process is also very error-prone, since silicate products are complex mixtures, and other hydration product components slowly decompose during 500-850 ℃ to cause mass loss; meanwhile, the method cannot distinguish whether the calcium carbonate is self-contained in the raw material or generated during the carbon fixation maintenance.|DISCLOSURE|Disclosure of Invention|[0007] The invention aims to solve the technical problems of large error and poor accuracy of the existing detection method, and provides a method for detecting the carbon dioxide content of silicate products by utilizing an infrared sulfur-carbon analyzer, which can realize quantitative detection of the carbon fixation amount of silicate products and has high accuracy and high reliability of detection results,|[0008] The technical problems to be solved by the method can be implemented by the following technical schemes.|[0009] A method for determining the fixed carbon dioxide content of a silicate product, comprising the steps of:|[0010] S1, sampling two groups of test blocks before and after carbon maintenance, respectively drying, crushing, grinding and sieving; to below 200 meshes; wherein 200 mesh is the expected grinding value (sample is expected to be no greater than 200 mesh, where 200 mesh is the expected value); during sieving, a square hole sieve with 0.04-0.08mm can be selected; |[0011] S2, crucible pretreatment: |[0012] the crucible is kept at 800-1400 ℃ for 1-4 h and is put into a dryer for preservation |[0013] S3, detecting by an infrared carbon-sulfur analyzer:|[0014] Weighing the sample prepared in the step S1, putting the sample into the crucible pretreated in the step S2, uniformly covering a fluxing agent on the crucible, and analyzing the sample on an infrared carbon-sulfur analyzer; |[0015] S4, calculating the carbon sequestration amount: |[0016] the difference of the carbon content before and after the carbon maintenance/the mass of the sample is the carbon fixation amount. |[0017] Further, the drying condition in step S1 is 105 ℃ to constant weight.|[0018] Further, the front and rear groups of test blocks in the step S1 are respectively taken from a batch of test blocks before and after the carbon fixing maintenance.|[0019] Preferably, in step S3, 1-3g of flux is uniformly covered every 0.1-0.5g of sample during weighing. Each sample was weighed and tested separately, and the two samples obtained were weighed in equal amounts before and after carbon fixation.|[0020] Further, in the step S1, after the sample is crushed to particles with the particle diameter of less than 10mm, sampling is carried out by a quartering method, and then grinding and sieving are carried out.|[0021] Further, in step S4, the carbon sequestration amount is calculated using the following formula:|[0022] |[0023] wherein, C: silicate product fixes carbon dioxide content% |[0024] C2: carbon content of sample after carbon fixation%|[0025] C1: carbon content of the sample before carbon fixation,%.|[0026] Further, the fluxing agent in the step S3 is one or a mixture of more than two of tungsten particles, tin particles and pure iron.|[0027] Preferably, the infrared carbon and sulfur analyzer is an HCS-500 infrared carbon and sulfur analyzer.|[0028] Preferably, the working conditions of the infrared carbon sulfur analyzer are as follows: carrier flow rate is 2-4L/min, carrier gas pressure is 30-40 psi, and dynamic air pressure is 35-45 psi.|[0029] Preferably, in step S3, the analysis time is 30 to 50 seconds, and the comparison level is 2 to 4.|[0030] Compared with the prior art, the invention has the following beneficial effects:|[0031] (1) The sample detected by the method is a test block before and after carbon fixation maintenance of the same batch of products, and is scientifically sampled by full crushing and a quartering method, and the sample is representative and can accurately reflect the carbon fixation amount in the carbon maintenance process. |[0032] (2) The sample pretreatment method provided by the invention adopts 105 ℃ drying to remove moisture and stop hydration, so that errors caused by the fact that products are continuously hydrated to generate new solid products are avoided; and the sealed air-insulated storage is adopted to avoid errors caused by carbon dioxide contact, and the device has the characteristic of high accuracy.|[0033] (3) The detection method provided by the invention has reliable results and high repeatability, and is suitable for the determination of solid carbon content of various silicate products.|INVENTION MODE|Detailed Description|[0034] The following detailed description of specific embodiments of the invention is provided in further detail.|[0035] The invention provides a method for measuring the fixed carbon dioxide content of silicate products by using an infrared carbon-sulfur analyzer, wherein the infrared carbon-sulfur analyzer used in the method is a full-automatic analyzer for analyzing the carbon and sulfur content in metals, ores, soil and other substances in the industries of metallurgy, machinery, chemical industry and the like, but the application of the infrared carbon-sulfur analyzer in the detection of the carbon content in silicate products is not seen at present. And because the raw materials of silicate products often have implicit carbon components, the carbon fixation amount cannot be represented by directly using the carbon content result of the test block after carbon fixation maintenance.|[0036] The following steps of the method are as follows:|[0037] (1) Pretreatment of a sample before carbon fixation: |[0038] randomly extracting 1-3 test blocks into 1 group in the same batch of test blocks before carbon fixation maintenance, immediately drying in a 105 ℃ oven until the weight is constant, respectively crushing each test block to 0-10mm particles, respectively sampling 25-100g of samples by a quartering method, grinding the samples, sieving with a 0.04-0.08mm square hole sieve, and sealing for later use; |[0039] (2) Sample pretreatment after carbon fixation maintenance: |[0040] randomly extracting 1-3 test blocks into 1 group from the same batch of test blocks after the carbon fixation maintenance is finished, immediately drying in a 105 ℃ oven until the weight is constant, respectively crushing all the test blocks to 0-10mm particles, respectively sampling 25-100g of samples by a quartering method, grinding the samples, sieving the samples by a square hole sieve of 0.04-0.08mm, and sealing for later use; |[0041] (3) Crucible pretreatment: |[0042] preserving the crucible at 800-1400 ℃ for 1-4 hours, and placing the crucible in a dryer for preservation; |[0043] (4) And (3) detecting by an infrared carbon-sulfur analyzer: |[0044] Weighing 0.1-0.5g of sample before and after curing of carbon fixation, placing the sample into a pretreated crucible, uniformly covering 1-3g of fluxing agent on the crucible, and analyzing the sample on an infrared carbon-sulfur analyzer. |[0045] (5) Calculation of carbon fixation: the formula for calculating the carbon fixation is as follows:|[0046] |[0047] wherein, C: silicate product fixes carbon dioxide content% |[0048] C2: carbon content of sample after carbon fixation%|[0049] C1: carbon content of sample before carbon fixation%|[0050] The average value of the fixed carbon dioxide content of 3 test pieces is taken as a final test result, and the test result is repaired to be about 2 bits after decimal places.|[0051] In the steps (1) and (2), 3 test blocks are randomly extracted from the same batch of test blocks after the carbon fixation maintenance is finished to form 1 group, the test blocks are immediately dried in a 105 ℃ oven until the weight is constant, each test block is respectively crushed to 0-10mm particles, 50-60g of samples are respectively sampled by a quartering method, and the samples are ground and then are sealed for later use after being screened by a square hole sieve of 0.04-0.08 mm;|[0052] Preferably, the temperature of the crucible pretreatment in the step (3) is 1000-1200 ℃, and the temperature is kept for 2-3 hours. |[0053] Preferably, in the step (4), the sample is weighed in an amount of 0.2 to 0.3g.|[0054] The fluxing agent in the step (4) is one or a mixture of more than two of tungsten particles, tin particles and pure iron. The flux is preferably weighed in an amount of 2-3g.|[0055] The infrared carbon and sulfur analyzer in the step (4) is preferably an HCS-500 infrared carbon and sulfur analyzer.|[0056] The working conditions of the infrared carbon-sulfur analyzer in the step (4) are as follows: carrier flow rate is 2-4L/min, carrier gas pressure is 30-40 psi, and dynamic air pressure is 35-45 psi.|[0057] The analysis time in the step (4) is 30-50 s, and the comparison level is 2-4.|[0058] The determination method provided by the invention solves the problems that the method for detecting the carbon content of silicate products is inaccurate and the requirement of quantitative detection cannot be met.|[0059] The method of determining the fixed carbon dioxide content of silicate articles of the present invention is further illustrated below in conjunction with specific examples, which are provided to illustrate the invention and are not intended to limit the scope of the invention.|[0060] Example 1|[0061] The method for determining the fixed carbon dioxide content of the silicate product provided by the embodiment mainly comprises the following steps:|[0062] (1) Pretreatment of a sample before carbon fixation: |[0063] Randomly extracting 3 test blocks into 1 group from the same batch of concrete test blocks before carbon fixation maintenance, immediately drying in a 105 ℃ oven until the weight is constant, crushing all the test blocks into particles below 10mm, respectively sampling 50g of samples by a quartering method, grinding, sieving with a 0.08mm square hole sieve, and sealing for later use; |[0064] (2) Sample pretreatment after carbon fixation maintenance: |[0065] Randomly extracting 3 test blocks into 1 group from the same batch of concrete test blocks after the carbon fixation maintenance is finished, immediately drying in a 105 ℃ oven until the weight is constant, crushing all the test blocks into particles below 10mm, respectively sampling 50g of samples by a quartering method, grinding, sieving by a square hole sieve of 0.08mm, and sealing for later use; |[0066] (3) Crucible pretreatment: |[0067] preserving the crucible at 1200 ℃ for 2 hours, and placing the crucible in a dryer for preservation; |[0068] (4) And (3) detecting by an infrared carbon-sulfur analyzer: |[0069] Weighing 0.2g of samples before and after carbon fixation maintenance, putting the samples into a crucible after pretreatment, uniformly covering 2g of fluxing agent on the samples, and analyzing the samples on an infrared carbon-sulfur analyzer; |[0070] (5) Calculation of carbon fixation: |[0071] The carbon content of the concrete sample before carbon fixation is 2.23%, 2.25% and 2.26%, and the carbon content of the concrete sample after carbon fixation is 2.58%, 2.59% and 2.56%, and the carbon content of the concrete sample after carbon fixation is 1.21% according to the formula. |[0072] Example 2|[0073] The method for determining the fixed carbon dioxide content of the silicate product provided by the embodiment mainly comprises the following steps:|[0074] (1) Pretreatment of a sample before carbon fixation: |[0075] randomly extracting 3 test blocks into 1 group in the same batch of autoclaved aerated concrete blocks before carbon fixing maintenance, immediately drying in a 105 ℃ oven until the weight is constant, crushing all the test blocks into particles below 5mm, respectively sampling 50g of samples by a quartering method, grinding, sieving with a 0.08mm square hole sieve, and sealing for later use; |[0076] (2) Sample pretreatment after carbon fixation maintenance: |[0077] Randomly extracting 3 test blocks into 1 group in the same batch of autoclaved aerated concrete blocks after the carbon fixation maintenance is finished, immediately drying in a 105 ℃ oven until the weight is constant, crushing all the test blocks into particles below 5mm, respectively sampling 50g of samples by a quartering method, grinding, sieving by a square hole sieve of 0.08mm, and sealing for later use; |[0078] (3) Crucible pretreatment: |[0079] preserving the crucible at 1000 ℃ for 3 hours, and placing the crucible in a dryer for preservation; |[0080] (4) And (3) detecting by an infrared carbon-sulfur analyzer: |[0081] Weighing 0.3g of samples before and after carbon fixation maintenance, putting the samples into a crucible after pretreatment, uniformly covering 2.5g of fluxing agent on the samples, and analyzing the samples on an infrared carbon-sulfur analyzer; |[0082] (5) Calculation of carbon fixation: |[0083] the carbon content of the autoclaved aerated concrete block sample before carbon fixation is 0.83%, 0.84% and 0.83%, and the carbon content of the autoclaved aerated concrete block sample after carbon fixation is 1.02%, 1.03% and 10.4%, and the fixed carbon dioxide content of the autoclaved aerated concrete block sample is calculated to be 0.72% according to a formula. |[0084] Example 3|[0085] The method for determining the fixed carbon dioxide content of the silicate product provided by the embodiment mainly comprises the following steps:|[0086] (1) Pretreatment of a sample before carbon fixation: |[0087] Randomly extracting 3 test blocks into 1 group in the same batch of cement boards before carbon fixation maintenance, immediately drying in a 105 ℃ oven until the weight is constant, completely crushing each test block into particles below 5mm, respectively sampling 60g of samples by a quartering method, grinding, sieving with a 0.04mm square hole sieve, and sealing for later use; |[0088] (2) Sample pretreatment after carbon fixation maintenance: |[0089] Randomly extracting 3 test blocks into 1 group from the same batch of cement boards after the carbon fixation maintenance is finished, immediately drying in a 105 ℃ oven until the weight is constant, completely crushing each test block into particles below 5mm, respectively sampling 60g of samples by a quartering method, grinding, sieving by a 0.04mm square hole sieve, and sealing for later use; |[0090] (3) Crucible pretreatment: |[0091] preserving the crucible at 1200 ℃ for 2 hours, and placing the crucible in a dryer for preservation; |[0092] (4) And (3) detecting by an infrared carbon-sulfur analyzer: weighing 0.2g of samples before and after carbon fixation maintenance, putting the samples into a pretreated crucible, uniformly covering 2g of fluxing agent on the samples, and analyzing the samples on an infrared carbon-sulfur analyzer. |[0093] (5) Calculation of carbon fixation: the carbon content of the cement board sample before carbon fixation is 4.21%, 4.19% and 4.22%, the carbon content of the cement board sample after carbon fixation is 5.12%, 5.13% and 5.13%, and the carbon content of the cement board sample after carbon fixation is 3.39% according to the formula.|[0094] Example 4 (non-preferred operation)|[0095] The selection of the sample weighing has a certain influence on the accuracy of analysis results. Too low a sample weight may result in a low sample representation, and too high a sample weight may result in incomplete carbon release from the sample and may result in a lower analysis result. The symmetrical sample amounts were tested using a standard sample having a carbon content of 1.00%.|[0096] The experimental process comprises the following steps: weighing 0.1-0.5 g of standard sample, placing the standard sample into a crucible pretreated for 2 hours at 1200 ℃, uniformly covering 2g of fluxing agent on the crucible, and analyzing the mixture on an infrared carbon-sulfur analyzer.|[0097] TABLE 1 influence of Standard sample Scale on detection results|[0098] Standard sample weighing gDetection value%Detection value%Detection value%Average%0.10.970.980.950.970.20.9811.000.990.30.9911.001.000.40.960.960.950.960.50.960.940.950.95|[0099] The sample amount is preferably 0.2 to 0.3g by comparison of the average value in table 1 and the carbon content of the standard sample.|[0100] Example 5 (non-preferred operation)|[0101] The choice of flux weighing also has a certain impact on the accuracy of the analysis results. The too low flux weighing amount can lead to insufficient sample combustion and lower analysis result; the flux is excessively high in sample weighing amount, so that the sample is easy to splash and redundant dust is easy to generate, and the analysis result is influenced. The symmetrical sample amounts were tested using a standard sample having a carbon content of 1.00%.|[0102] The experimental process comprises the following steps: 0.2g of standard sample is weighed, placed in a crucible pretreated for 2 hours at 1200 ℃, evenly covered with 1-5 g of fluxing agent, and analyzed on an infrared carbon-sulfur analyzer.|[0103] TABLE 2 influence of flux sample weights on detection results|[0104] Flux weighing gDetection value%Detection value%Detection value%Average%1.00.940.950.950.952.00.980.991.000.993.01.000.991.001.004.00.940.950.940.945.00.930.940.930.93|[0105] The sample amount is preferably 2 to 3g by comparison of the average value in table 2 and the carbon content of the standard sample.|[0106] The previous description of the embodiments is provided to facilitate a person of ordinary skill in the art in order to make and use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments, and those skilled in the art, based on the principle of the present invention, should make improvements and modifications without departing from the scope of the present invention. Family Number|(111335901)|111335901|Abstract|(CN118603924 A)|The invention provides a method for determining the fixed carbon dioxide content of a silicate product , which comprises the following steps : S1 , sampling two groups of test blocks before and after carbon maintenance , drying , crushing and grinding to below 200 meshes ; s2 , crucible pretreatment : carrying out heat preservation on the crucible at 800-1400 DEG C for 1-4 hours , and storing the crucible in a dryer ; s3 , detecting by an infrared carbon - sulfur analyzer : weighing the sample prepared in the step S1 , putting the sample into the crucible pretreated in the step S2 , uniformly covering the crucible with a fluxing agent , and analyzing on the infrared carbon - sulfur analyzer ; s4 , calculating the carbon sequestration amount , wherein the ratio of the carbon content difference value before and after carbon maintenance to the sample mass is the carbon sequestration amount . |CPC codes|(CN118603924 A)|G01N - 001/28/6 |G01N - 001/34 |G01N - 001/44 |G01N - 021/35/63 |G01N - 2001/2866 |G01N - 2021/3572 |IPC codes|(CN118603924 A)|G01N - 001/28 |G01N - 001/34 |G01N - 001/44 |G01N - 021/3563 | Measurement G01N-001/28/6|G01N-001/34|G01N-001/44|G01N-021/35/63|G01N-2001/2866|G01N-2021/3572 G01N-001/28/6|G01N-001/34|G01N-001/44|G01N-021/35/63|G01N-2001/2866|G01N-2021/3572 G01N-001/28|G01N-001/34|G01N-001/44|G01N-021/3563 G01N-001/28|G01N-001/34|G01N-001/44|G01N-021/3563 PENDING (CN118603924)|PENDING ALIVE (CN118603924)|ALIVE (CN118603924)|LEGAL DETAILS FOR CN118603924|Actual or expected expiration date=2044-05-23|Legal state=ALIVE|Status=PENDING|Event publication date=2024-05-23|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202410643788|Application date=2024-05-23|Standardized application number=2024CN-0643788|Event publication date=2024-09-06|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN118603924|Publication stage code=A|Publication date=2024-09-06|Standardized publication number=CN118603924|Event publication date=2024-09-06|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-09-24|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN118603924)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSfyGjXxbAagFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000074389020&ekey=2002&xpn=CN118603924&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=u5OShd81oxx2S8XOCqJJKZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN118603924)|CN (CN118603924)|NAME=SHANGHAI RESEARCH INSTITUTE OF BUILDING SCIENCES CO., LTD , COUNTRY=CN (CN118603924)|NAME=CAI JIAJIE;SHANGHAI JIUZE LAWYER AFFAIRS , REG=31337 (CN118603924)|NAME=LIN MAOSONG|NAME=YANG GUANG|NAME=YANG LIXIANG|NAME=WANG QIONG 0 1 Titre: (CN118603924)|Method for measuring fixed carbon dioxide content of silicate product Résumé: (CN118603924)|The invention provides a method for determining the fixed carbon dioxide content of a silicate product, which comprises the following steps: S1, sampling two groups of test blocks before and after carbon maintenance, drying, crushing and grinding to below 200 meshes; s2, crucible pretreatment: carrying out heat preservation on the crucible at 800-1400 DEG C for 1-4 hours, and storing the crucible in a dryer; s3, detecting by an infrared carbon-sulfur analyzer: weighing the sample prepared in the step S1, putting the sample into the crucible pretreated in the step S2, uniformly covering the crucible with a fluxing agent, and analyzing on the infrared carbon-sulfur analyzer; s4, calculating the carbon sequestration amount, wherein the ratio of the carbon content difference value before and after carbon maintenance to the sample mass is the carbon sequestration amount. 83 Abstract gpt-4o-mini no The article focuses on a method for measuring fixed carbon dioxide content in silicate products, rather than on processes or technologies aimed at enhancing weathering or carbon sequestration.
85 CN201710377733 CN201710377733 CN107089665|CN107089665 77100625 CN107089665 B 2023-05-16 [CN107089665B]|CN107089665 A 2017-08-25 [CN107089665] 2017-05-25 2017-05-25 2023-05-16|2017-08-25 (CN107089665B)|2023-05-16 (CN107089665)|2037-05-25 (CN107089665)|Crystalline silicon purification integrated system (CN107089665)|The invention discloses a crystalline silicon purification integrated system which comprises a first crushing device, a pickling device, a raw silicon ore smelting electric furnace, a second crushing device, a carbon removal device and an electron-beam smelting device. Crude silicon is crushed by the first crushing device, and the crushed material is pickled by the pickling device and then subjected to wash heat smelting by utilizing the raw silicon ore smelting electric furnace so as to obtain the raw silicon. After the raw silicon is crushed by the second crushing device, the raw silicon is calcined by the carbon removal device so as to reduce the carbon content in the crushed material produced by the second crushing device, the calcined crushed material is subjected to smelting phosphorous removal by the electron-beam smelting device, the raw materials subjected to phosphorous removal are scanned and heated in an area-variable surface scanning manner and according to a first preset power, and then the impurities are continuously gathered and volatilized into a molten bath by utilizing a solid-liquid interface between the molten bath and the crystallized materials. An electron beam gun is controlled to obtain semi-finished polycrystalline silicon in the area-variable surface scanning manner and at gradually decreased power, and the bottom and top impurity enrichment areas of the semi-finished polycrystalline silicon are sawed so as to obtain the polycrystalline silicon. NINGXIA DONGMENG ENERGY (CN107089665)|NINGXIA DONGMENG ENERGY CO LTD ([CN])|(CN107089665)|NINGXIA DONGMENG ENERGY CO LTD LIU YINGKUAN|WEN WEIDONG|FENG QUANYI|ZHOU XUEMEI|YANG QI|LU ZANDONG|YAN GANG|LI YANG|JIANG LIHUA|SUO XIAOFENG (CN107089665)|LIU YINGKUAN|WEN WEIDONG|FENG QUANYI|ZHOU XUEMEI|YANG QI|LU ZANDONG|YAN GANG|LI YANG|JIANG LIHUA|SUO XIAOFENG|(CN107089665)|LIU YINGKUAN|WEN WEIDONG|FENG QUANYI|ZHOU XUEMEI|YANG QI|LU ZANDONG|YAN GANG|LI YANG|JIANG LIHUA|SUO XIAOFENG (CN107089665)|SUN YANHU;NINGXIA SANYUANXIN INTELLECTUAL PROPERTY AGENCY FIRM (GENERAL PARTNERSHIP)|Reg. Nb: 64105 (CN107089665)|The existing technology for purifying and integrating solar-grade polysilicon prepared by a metallurgical method has the advantages of better quality, lower energy consumption and environmental friendliness, but the comprehensive cost is still higher, and the market share of the product is very small.| (CN107089665)|1. A crystalline silicon purification integrated system, comprising: the device comprises a first crushing device, an acid washing device, a raw material silicon ore heating furnace, a second crushing device, a carbon removal device and an electron beam smelting device; crushing the crude silicon material to 30-150 meshes by a first crushing device to obtain a first crushed material; the acid washing device carries out acid washing on the first crushed material produced by the first crushing device so as to remove impurities on the surface of the first crushed material; the method comprises the steps that a raw material silicon ore heating furnace adopts a submerged arc smelting mode to carry out first crushed materials after pickling and impurity removal of a slag pickling smelting pickling device so as to obtain raw material silicon; crushing the raw material silicon produced by the raw material silicon ore heating furnace by a second crushing device to obtain a second crushed material, wherein the mesh number of the second crushed material is 30-150 meshes; the carbon removing device is used for calcining the second crushed material produced by the second crushing device to reduce the carbon content in the second crushed material, wherein the carbon content in the calcined second crushed material is less than 0.4ppm; the electron beam smelting device comprises a control device, a feeding device, a furnace body, two smelting crucibles arranged in the furnace body, a water-cooling copper crucible and electron beam guns correspondingly arranged above the smelting crucibles and the water-cooling copper crucible, wherein the control device controls the feeding device, the smelting crucibles, the water-cooling copper crucible and the electron beam guns to work; the area-changing surface scanning mode is to adjust the frequency of expanding and shrinking the scanning surface of the electron beam, so that the scanned area in the water-cooled copper crucible is continuously changed from large to small to realize the control of the moving speed and the crystallization speed of the melting zone; after the raw materials in the water-cooled copper crucible are full, the control device controls the electron beam gun above the water-cooled copper crucible to reduce the power and concentrate impurities in the silicon ingot to the center of the top of the silicon ingot in a surface scanning mode with unchanged area and gradually reduce the power, the silicon ingot in the water-cooled copper crucible is cooled and then is discharged to obtain a semi-finished polysilicon product, and the bottom and top impurity enrichment areas of the semi-finished polysilicon product are sawed to obtain polysilicon; wherein, the control device controls the charging device to add the second crushed material after the calcination of predetermined amount into two smelting crucibles, and the control device controls the electron beam gun above two smelting crucibles to smelt the specific process of dephosphorization to the second crushed material in two smelting crucibles: the control device controls the feeding device to feed a unit amount of second crushed material into each smelting crucible each time, controls the electron beam gun to smelt the unit amount of second crushed material according to the first preset power for a first preset time period, then feeds the unit amount of second crushed material into the smelting crucible and controls the electron beam gun to smelt the unit amount of second crushed material fed into the smelting crucible for the first preset time period according to the first preset power, until the control device calculates that the amount of the second crushed material fed into the smelting crucible corresponds to the preset amount, and then smelts the second preset time period, and then controls the two smelting crucibles to flow molten raw materials into the water-cooled copper crucible alternately, and the time difference of the two smelting crucible flows is a third preset time period.| (CN107089665)|A crystalline silicon purification integration system comprising: the device comprises a first crushing device, an acid washing device, a raw material silicon ore heating furnace, a second crushing device, a carbon removal device and an electron beam smelting device; crushing the crude silicon material by a first crushing device, and carrying out slag washing smelting by using a raw material silicon ore heating furnace after pickling the crushed material by a pickling device to obtain raw material silicon.|The invention relates to the technical field of polysilicon production, in particular to a crystalline silicon purification integrated system.| (CN107089665)|SMELTING CRUCIBLE(100,28)|CRYSTALLINE SILICON PURIFICATION(100,20)|ORE HEATING FURNACE(54,10)|CRUSHING(48,33)|CORUNDUM CASTABLE REFRACTORY LAYER(44,3)|COPPER CRUCIBLE(40,35)|CRYSTALLINE SILICON PURIFICATION INTEGRATION(40,1)|SUBMERGED ARC SMELTING(38,7)|SMELTING PICKLING(35,2)|SILICON PURIFICATION INTEGRATION(35,1)|CRUSHED MATERIAL(34,75)|SLAG IMPURITY REMOVAL(33,1)|ELECTRON BEAM SMELTING(31,12)|WASHING SMELTING RECTANGLE(31,3)|ACID WASHING(27,7)|RAW SILICON(26,4)|WASHING SMELTING(26,2)|FURNACE(25,24)|ELECTRON BEAM GUN(22,12)|SUBMERGED ARC(22,7)|ELECTRON BEAM(21,35)|WATER COOLED COPPER CRUCIBLE(20,35)|WATER COOLING COPPER CRUCIBLE(20,6)|COPPER CRUCIBLE TUBE(20,2)|SOLAR GRADE POLYSILICON(20,2)|FRIENDLINESS(20,1)|PICKLING(19,6)|IMPURITY ENRICHMENT AREA(19,5)|SMELTING CRUCIBLE FLOW(19,2)|PRESET POWER(18,8)|IMPURITY RECTANGLE(18,5)|ACID WASHING RECTANGLE(18,2)|COMPREHENSIVE COST(18,1)|CARBON CONTENT(17,9)|REMOVING CARBON(17,5)|DEPHOSPHORIZATION(17,2)|POLYSILICON PRODUCTION(16,7)|QUANTITATIVE SLAG(16,2)|SILICON INGOT(15,20)|IMPURITY(15,8)|ORE SMELTING FURNACE(15,5)|MELTING ZONE(15,3)|RAW MATERIAL SILICON(14,36)|ELECTRODE PILE ARRANGED RECTANGLE(14,1)|REMOVING IMPURITY(13,5)|UNCHANGED AREA(13,5)|MOLTEN POOL THICKNESS(13,2)|SILICON SLAG INTERFACE(13,2)|CRYSTALIZATION(12,3)|POLYSILICON PRODUCTION TUBE(12,3)|AMOUNT CALCINATION(12,2)|SMELT(12,2)|ELECTRODE PASTE LAYER(11,6)|SEMI FINISHED POLYSILICON PRODUCT(11,5)|SEMI FINISHED PRODUCT(11,2)|POLYSILICON(10,7)|SCANNING MODE(10,4)|CALCINED CRUSHED MATERIAL(10,1)|SILICON INGOT TUBE(9,1)|SCANNED AREA(8,3)|SLAG LIQUID(8,3)|ARCING(8,1)|TUBE ARRANGED RECTANGLE(8,1)|PRESET TIME PERIOD(7,11)|SURFACE SCANNING MODE(7,11)|ACID PICKLING RECTANGLE(7,4)|MOVING SPEED(7,3)|DEPHOSPHORIZED RAW MATERIAL(7,1)|GRADUALLY REDUCING POWER(7,1)|SMELTING DEPHOSPHORIZATION RECTANGLE(7,1)|MATERIAL CRYSTAL(6,2)|TOP IMPURITY ENRICHMENT AREA(5,4)|FURNACE BOTTOM(5,3)|WHITE CORUNDUM(5,3)|SCANNING AREA(5,2)|SLAG WASHING SMELTING(5,1)|ENERGY CONSUMPTION(4,7)|MOLTEN RAW MATERIAL(4,4)|FACILITATED CRUCIBLE VOLUME(4,2)|SILICON CRUCIBLE(4,2)|SILICON IMPURITY(4,2)|SOLAR GRADE POLYCRYSTALLINE SILICON(4,2)|ABSOLUTE SHARE MARKET(4,1)|INGOT FURNACE DIRECTIONAL SOLIDIFICATION(4,1)|OPERATION RECTANGLE(4,1)|PICKLING IMPURITY REMOVAL(4,1)|RAW SILICON ORE FURNACE(4,1)|REFRACTORY LAYER(3,3)|CHANGING AREA(3,2)|DISCONTINUOUS MATERIAL(3,2)|HYDROMETALLURGY(3,2)|MASS RATIO(3,2)|PHOSPHORUS REMOVAL(3,2)|SOLID LIQUID INTERFACE(3,2)|ARC STRIKING(3,1)|CALCINATION RECTANGLE(3,1)|COMPREHENSIVE ELECTRICITY CONSUMPTION(3,1)|MOLTEN BATH(3,1)|POLYCRYSTALLINE SILICON INGOT(3,1)|QUALITY REQUIREMENT RECTANGLE(3,1)|REFRACTORY STONE(3,1)|STACKING CARBON BRICK(3,1)|CONTROL DEVICE(2,35)|INNER WALL(2,5)|PRODUCTION COST(2,4)|SHORT SERVICE LIFE(2,2)|CASTABLE DISPOSED RECTANGLE(2,1)|DECARBONIZING(2,1)|EQUIPMENT INVESTMENT(2,1)|HOT SLAG(2,1)|IMPURITY TUBE(2,1)|MODULE FUNCTION(2,1)|PRIMARY FINISHING(2,1)|PRODUCTION TON(2,1)|SPECIAL INDUSTRIAL SILICON REQUIREMENT(2,1)|TON POLYSILICON POWER CONSUMPTION(2,1)|VACUUM DIRECTIONAL SOLIDIFICATION(2,1)||(CN107089665)|MELTING CRUCIBLE(100,57)|CRYSTALLINE SILICON PURIFICATION(100,17)|COPPER CRUCIBLE(94,58)|CRUSHING(72,33)|MOLTEN POOL(66,19)|ORE HOT FURNACE(65,5)|SUBMERGED ARC SMELTING(53,7)|CORUNDUM CASTABLE REFRACTORY LAYER(50,7)|WATER COOLED COPPER CRUCIBLE(48,58)|ELECTRON BEAM GUN(45,22)|SMELTING CRUCIBLE(45,7)|ORE HEATING FURNACE(43,12)|WASHING SMELTING(43,7)|CRUSHED MATERIAL(42,78)|FURNACE(37,25)|REMOVING CARBON(36,8)|ELECTRON BEAM SMELTING(34,5)|SMELTING DEPHOSPHORIZATION(32,2)|IMPURITY(31,20)|SUBMERGED ARC(31,7)|PICKLING(31,5)|IMPURITY ENRICHMENT REGION(29,4)|IMPURITY ENRICHED REGION(28,1)|ACIDIC WASH(27,14)|CARBON CONTENT(27,9)|COARSE SILICON(27,2)|POLYSILICON PRODUCTION(26,6)|ACID WASHING(25,10)|SEMI FINISHED POLYSILICON PRODUCT(24,6)|CALCINED CRUSHED MATERIAL(24,1)|ELECTRON BEAM(23,23)|SCANNING MODE(23,5)|PHOSPHORUS(23,4)|QUANTITATIVE SLAG(23,2)|POLYCRYSTALLINE SILICON(22,13)|PRESET POWER(21,8)|MELTING ZONE(21,3)|RAW MATERIAL SILICON(20,37)|SILICON INGOT(20,14)|SMELTING(19,6)|MOLTEN POOL THICKNESS(19,2)|SILICON SLAG INTERFACE(19,2)|CRYSTALIZATION(18,3)|ELECTRODE PILE(18,3)|SCANNING REDUCTION(18,3)|CALCINATION(17,3)|POLYSILICON(17,3)|SEMI FINISHED PRODUCT(16,6)|UNCHANGED AREA(16,3)|SCAN(16,1)|ELECTRODE PASTE LAYER(15,7)|MATERIAL CRYSTAL(15,6)|PRESET THICKNESS(15,5)|INGOT(14,5)|DEVICE MELT(13,1)|SURFACE SCANNING MODE(12,14)|DISCONTINUOUS MATERIAL(12,4)|FURNACE BOTTOM(12,4)|TOP IMPURITY ENRICHMENT REGION(12,4)|SCANNED AREA(12,3)|MOVING SPEED(11,2)|COARSE SILICON MATERIAL(10,5)|ELECTRON BEAM MELTING(9,11)|SOLID LIQUID INTERFACE(9,6)|CHANGING AREA(9,4)|SOLAR GRADE POLYSILICON(9,2)|INGOT FURNACE(8,3)|GRADUALLY REDUCING POWER(8,2)|PRESET TIME PERIOD(7,8)|MOLTEN RAW MATERIAL(7,7)|SCANNING AREA(7,2)|FIXED AREA(6,5)|RAW MATERIAL(5,10)|DIRECTIONAL SOLIDIFICATION PURIFICATION(5,2)|MAINSTREAM STATUS(5,1)|MARKET ABSOLUTE SHARE(5,1)|ORE SMELTING FURNACE(5,1)|PHOSPHORUS REMOVED RAW MATERIAL(5,1)|REFRACTORY STONE(5,1)|SOLAR GRADE POLYCRYSTALLINE SILICON(5,1)|STACKING CARBON BRICK(5,1)|METALLIC IMPURITY(4,3)|HYDROMETALLURGY(4,2)|MODULE FUNCTION(4,2)|PHOSPHORUS REMOVAL(4,2)|REMOVING IMPURITY(4,2)|BUILDING FURNACE(4,1)|CRYSTALLINE SILICON PHOTOVOLTAICS(4,1)|MAJOR NATIONAL SCIENCE(4,1)|ORE FURNACE(4,1)|CONTROL DEVICE(3,48)|INNER WALL(3,5)|MASS RATIO(3,3)|QUALITY REQUIREMENT(3,2)|SHORT SERVICE LIFE(3,2)|CUTTING IMPURITY REMOVAL(3,1)|DEMONSTRATION(3,1)|EQUIPMENT INVESTMENT(3,1)|HOT FURNACE SLAG(3,1)|POLYCRYSTALLINE SILICON ELECTRICITY CONSUMPTION(3,1)|PRIMARY FINISHING(3,1)|SILICON WASTE(3,1)|TECHNICAL INDEX(3,1)|VACUUM DIRECTIONAL SOLIDIFICATION(3,1)|CARRYING OUT ACID WASHING(2,2)| (CN107089665)|1. A crystalline silicon purification integrated system, comprising: the device comprises a first crushing device, an acid washing device, a raw material silicon ore heating furnace, a second crushing device, a carbon removal device and an electron beam smelting device; crushing the crude silicon material to 30-150 meshes by a first crushing device to obtain a first crushed material; the acid washing device carries out acid washing on the first crushed material produced by the first crushing device so as to remove impurities on the surface of the first crushed material; the method comprises the steps that a raw material silicon ore heating furnace adopts a submerged arc smelting mode to carry out first crushed materials after pickling and impurity removal of a slag pickling smelting pickling device so as to obtain raw material silicon; crushing the raw material silicon produced by the raw material silicon ore heating furnace by a second crushing device to obtain a second crushed material, wherein the mesh number of the second crushed material is 30-150 meshes; the carbon removing device is used for calcining the second crushed material produced by the second crushing device to reduce the carbon content in the second crushed material, wherein the carbon content in the calcined second crushed material is less than 0.4ppm; the electron beam smelting device comprises a control device, a feeding device, a furnace body, two smelting crucibles arranged in the furnace body, a water-cooling copper crucible and electron beam guns correspondingly arranged above the smelting crucibles and the water-cooling copper crucible, wherein the control device controls the feeding device, the smelting crucibles, the water-cooling copper crucible and the electron beam guns to work; the area-changing surface scanning mode is to adjust the frequency of expanding and shrinking the scanning surface of the electron beam, so that the scanned area in the water-cooled copper crucible is continuously changed from large to small to realize the control of the moving speed and the crystallization speed of the melting zone; after the raw materials in the water-cooled copper crucible are full, the control device controls the electron beam gun above the water-cooled copper crucible to reduce the power and concentrate impurities in the silicon ingot to the center of the top of the silicon ingot in a surface scanning mode with unchanged area and gradually reduce the power, the silicon ingot in the water-cooled copper crucible is cooled and then is discharged to obtain a semi-finished polysilicon product, and the bottom and top impurity enrichment areas of the semi-finished polysilicon product are sawed to obtain polysilicon; wherein, the control device controls the charging device to add the second crushed material after the calcination of predetermined amount into two smelting crucibles, and the control device controls the electron beam gun above two smelting crucibles to smelt the specific process of dephosphorization to the second crushed material in two smelting crucibles: the control device controls the feeding device to feed a unit amount of second crushed material into each smelting crucible each time, controls the electron beam gun to smelt the unit amount of second crushed material according to the first preset power for a first preset time period, then feeds the unit amount of second crushed material into the smelting crucible and controls the electron beam gun to smelt the unit amount of second crushed material fed into the smelting crucible for the first preset time period according to the first preset power, until the control device calculates that the amount of the second crushed material fed into the smelting crucible corresponds to the preset amount, and then smelts the second preset time period, and then controls the two smelting crucibles to flow molten raw materials into the water-cooled copper crucible alternately, and the time difference of the two smelting crucible flows is a third preset time period.|2. The crystalline silicon purification integrated system of claim 1, wherein: the predetermined amount is 24kg, the unit amount of silicon material is 2kg, the first predetermined power is 300KW, the first predetermined period of time is 2 minutes, the second predetermined period of time is 6 minutes, and the third predetermined period of time is 15 minutes.|3. The crystalline silicon purification integrated system of claim 2, wherein: the thickness of the molten pool is 3-5 cm.|4. The crystalline silicon purification integrated system of claim 3, wherein: after the raw material in the water-cooled copper crucible is full, the control device controls the electron beam gun above the water-cooled copper crucible to reduce the power in a surface scanning mode with unchanged area and gradually reduce the power, and when impurities in the silicon ingot are concentrated to the center of the top of the silicon ingot, the control device controls the power of the electron beam gun above the water-cooled copper crucible to gradually reduce until the power is reduced to 5kw, wherein the scanning area of the surface scanning mode is a circle with the diameter of 10 cm.|5. The crystalline silicon purification integrated system as recited in claim 4 wherein: the raw material silicon ore smelting furnace comprises a furnace body, electrodes, a white corundum castable refractory layer and an electrode paste layer, wherein the white corundum castable refractory layer and the electrode paste layer are arranged on the inner wall of the furnace body, the electrode paste layer is arranged between the inner wall of the furnace body and the white corundum castable refractory layer, a furnace bottom made of electrode paste and an electrode pile arranged on the furnace bottom are arranged under the electrodes, the electrodes and the electrode pile are matched to carry out slag washing smelting on a first crushed material in the furnace body to obtain raw material silicon, a slag flowing channel is formed in the middle of the furnace body, slag liquid flows out from a high-temperature area above a silicon slag interface in the furnace body by utilizing the slag flowing channel, and quantitative slag flowing and slag blocking are realized by plugging the slag flowing channel.|6. The crystalline silicon purification integrated system as recited in claim 5 wherein: the specific process of carrying out slag washing smelting on the first crushed material in the furnace body by matching the electrode with the electrode pile to obtain raw material silicon comprises the following steps: mixing the first crushed material and the silicon slag according to the mass ratio of 1:1 to obtain a silicon slag mixture; firstly filling 200kg of silicon material under the electrode, quantitatively adding silicon slag mixture after arcing and melting, and smelting in a submerged arc smelting mode; when the mixture in the furnace body is completely melted, slag liquid is discharged through a slag flowing channel in a high temperature state, then slag is continuously added for smelting, the slag liquid is continuously discharged, slag washing operation on the first broken material is completed, and raw material silicon is obtained. (CN107089665)|TECHNICAL FIELD|[0001] The invention relates to the technical field of polysilicon production, in particular to a crystalline silicon purification integrated system.|BACKGROUND ART|[0002] Since human beings enter the new century, photovoltaic power generation has been rapidly developed, photovoltaic power generation equipment prepared by taking crystalline silicon as a raw material is widely used, crystalline silicon photovoltaic maintains the mainstream position of solar photovoltaic power generation in a quite long time, the main raw material of the crystalline silicon photovoltaic power generation is solar grade polycrystalline silicon, along with the rapid development of the photovoltaic power generation, the preparation of the polycrystalline silicon is more and more highly required in the aspects of quality, energy consumption, environment, cost and the like, and the aim is to continuously adapt to the requirements of photovoltaic power generation on low price surfing.|[0003] The method for preparing solar grade polysilicon mainly comprises an improved Siemens method (chemical method), a silane method (chemical method), a metallurgical method and the like. The improved Siemens method occupies the market of absolute share, but the cost is about 120 yuan/kg, and the difficulty in reduction is still larger.|[0004] The existing technology for purifying and integrating solar-grade polysilicon prepared by a metallurgical method has the advantages of better quality, lower energy consumption and environmental friendliness, but the comprehensive cost is still higher, and the market share of the product is very small. The existing process route is as follows: specially-produced industrial silicon, simple directional solidification, hydrometallurgy I, slag washing refining, simple directional solidification, hydrometallurgy II, vacuum directional solidification, primary finishing, electron beam smelting and secondary finishing. The technical indexes are as follows: less than or equal to 0.1ppm of B, less than or equal to 0.1ppm of P, less than or equal to 0.1ppm of metal impurities, less than or equal to 0.4ppm of C, less than or equal to 1ppm of O, and resistivity: 0.8-3.0 Ω CM, minority carrier lifetime: more than or equal to 3 mu s, the photoelectric conversion efficiency is more than or equal to 17.5 percent, and the comprehensive power consumption is as follows: 58kwh/kg, direct production cost: 138 yuan/kg.|[0005] The above-mentioned prior art has the technical problems of longer process route, higher energy consumption and higher production cost, for example: the requirements on raw materials are high, and special industrial silicon needs to be produced, so that the quality requirements on silica, petroleum coke and the like are high; the high temperature required for removing boron causes high requirements on crucible materials, small crucible volume, short service life and low yield per furnace; the ingot furnace is utilized for directional solidification and purification, so that the time is long, the energy consumption is high, the investment is large, and the yield is low; the electron beam dephosphorization process has long design time and high energy consumption.|DISCLOSURE|Disclosure of Invention|[0006] In view of the foregoing, it is desirable to provide a crystalline silicon purification integrated system that has a short process route and reduced energy consumption and production costs.|[0007] A crystalline silicon purification integrated system comprising: the device comprises a first crushing device, an acid washing device, a raw material silicon ore heating furnace, a second crushing device, a carbon removal device and an electron beam smelting device; the first crushing device crushes the crude silicon material to 30 to 150 meshes to obtain a first crushed material. The acid washing device carries out acid washing on the first crushed material produced by the first crushing device so as to remove impurities on the surface of the first crushed material. The raw material silicon ore heating furnace adopts a submerged arc smelting mode to carry out the first crushed material after the slag washing smelting pickling device is used for pickling and removing impurities so as to obtain raw material silicon. The second crushing device crushes the raw material silicon produced by the raw material silicon ore heating furnace to obtain a second crushed material, and the mesh number of the second crushed material is 30-150 meshes. The carbon removing device calcines the second crushed material produced by the second crushing device to reduce the carbon content in the second crushed material, wherein the carbon content in the calcined second crushed material is less than 0.4ppm. The electron beam smelting device comprises a control device, a feeding device, a furnace body, two smelting crucibles arranged in the furnace body, a water-cooling copper crucible and electron beam guns correspondingly arranged above the smelting crucibles and the water-cooling copper crucible, wherein the control device controls the feeding device, the smelting crucibles, the water-cooling copper crucible and the electron beam guns to work; the area-changing surface scanning mode is to adjust the frequency of expanding and shrinking the scanning surface of the electron beam, so that the scanned area in the water-cooled copper crucible is continuously changed from large to small to realize the control of the moving speed and the crystallization speed of the melting zone; after the raw materials in the water-cooled copper crucible are full, the control device controls the electron beam gun above the water-cooled copper crucible to reduce the power and concentrate impurities in the silicon ingot to the center of the top of the silicon ingot in a surface scanning mode with unchanged area and gradually reduce the power, the silicon ingot in the water-cooled copper crucible is cooled and then is discharged to obtain a semi-finished polysilicon product, and the bottom and top impurity enrichment areas of the semi-finished polysilicon product are sawed to obtain polysilicon; wherein, the control device controls the charging device to add the second crushed material after the calcination of predetermined amount into two smelting crucibles, and the control device controls the electron beam gun above two smelting crucibles to smelt the specific process of dephosphorization to the second crushed material in two smelting crucibles: the control device controls the feeding device to feed a unit amount of second crushed material into each smelting crucible each time, controls the electron beam gun to smelt the unit amount of second crushed material according to the first preset power for a first preset time period, then feeds the unit amount of second crushed material into the smelting crucible and controls the electron beam gun to smelt the unit amount of second crushed material fed into the smelting crucible for the first preset time period according to the first preset power, until the control device calculates that the amount of the second crushed material fed into the smelting crucible corresponds to the preset amount, and then smelts the second preset time period, and then controls the two smelting crucibles to flow molten raw materials into the water-cooled copper crucible alternately, and the time difference of the two smelting crucible flows is a third preset time period.|[0008] In the crystalline silicon purification integrated system, the first crushing device crushes crude silicon materials to 30-150 meshes to obtain first crushed materials, the acid pickling device performs acid pickling on the first crushed materials produced by the first crushing device to remove impurities on the surfaces of the first crushed materials, the raw material silicon ore heating furnace adopts a submerged arc smelting mode to perform slag washing smelting and acid pickling on the first crushed materials subjected to impurity removal by the acid pickling device to obtain raw material silicon, the second crushing device crushes the raw material silicon produced by the raw material silicon ore heating furnace to obtain second crushed materials, the mesh number of the second crushed materials is 30-150 meshes, the carbon removal device calcines the second crushed materials produced by the second crushing device to reduce the carbon content in the second crushed materials, the control device of the electron beam gun of the electron beam smelting device controls the second crushed materials in the two smelting crucibles to perform phosphorus removal and controls the two smelting crucibles to alternately flow into the water-cooled copper crucible, the control device controls the electron beam gun above the electron beam gun of the electron beam smelting device to control the water-cooled copper crucible to scan in a surface changing area mode, the power of the water-cooled copper ingot is controlled to be concentrated to the top of a polycrystalline silicon ingot, the silicon ingot is concentrated in a water-cooled area is ensured to be concentrated by the water-cooled silicon ingot, and the water-cooled silicon ingot is concentrated in the top of the water-cooled crucible is not controlled to be concentrated to be in the water-cooled silicon ingot after the top surface is concentrated to be concentrated with the water-cooled silicon ingot is in the water-cooled silicon ingot is concentrated by the water-cooled surface area, and the silicon impurity is concentrated down to be concentrated down to the silicon impurity is concentrated down to the silicon solution in the silicon crucible is concentrated down to the silicon crucible, to obtain polysilicon. And further solves the technical problems of longer process route, higher energy consumption and higher production cost in the prior art.|DRAWINGS DESCRIPTION|[0009] FIG. 1 is a schematic diagram showing the connection of functional blocks of a crystalline silicon purification integrated system according to a preferred embodiment.|[0010] Fig. 2 is a schematic structural view of the raw material silicon ore furnace of fig. 1.|[0011] Fig. 3 is a schematic diagram illustrating connection of functional modules of the electron beam melting apparatus of fig. 1.|[0012] In the figure: the integrated system 10 for purifying crystalline silicon comprises a first crushing device 11, a pickling device 12, a raw material silicon ore smelting furnace 13, a furnace body 131, an electrode 132, a refractory layer 133 of white corundum castable, an electrode paste layer 134, a furnace bottom 135, an electrode pile 136, a slag flow channel 137, a silicon liquid outflow channel 138, a second crushing device 14, a carbon removing device 15, an electron beam smelting device 16, a control device 161, a feeding device 162, a furnace body 163, a smelting crucible 164, a water-cooled copper crucible 165 and an electron beam gun 166.|INVENTION MODE|Detailed Description|[0013] Referring to fig. 1, the integrated system 10 for purifying crystalline silicon includes a first crushing device 11, an acid washing device 12, a raw silicon ore furnace 13, a second crushing device 14, a decarbonizing device 15, and an electron beam melting device 16.|[0014] The first crushing device 11 crushes the crude silicon material to 30 to 150 mesh to obtain a first crushed material. Coarse silicon materials are defined as 553 industrial silicon as well as silicon scrap, that is to say various silicon materials with a purity of more than 99%.|[0015] The acid washing device 12 washes the first crushed material produced by the first crushing device 11 to remove impurities on the surface of the first crushed material. Further, the pickling device 12 performs pickling on the polysilicon which is produced by the electron beam melting device 16 and is subjected to impurity removal by a saw.|[0016] The raw material silicon ore furnace 13 performs slag washing, smelting and pickling of the first crushed material after pickling and impurity removal of the pickling device 12 in a submerged arc smelting manner to obtain raw material silicon. Referring to fig. 2, the raw material silicon ore smelting furnace 13 includes a furnace body 131, electrodes 132, a refractory layer 133 of white corundum castable disposed on an inner wall of the furnace body 131, an electrode paste layer 134 and a furnace bottom 135 made of electrode paste, wherein the electrode paste layer 134 is disposed between the inner wall of the furnace body 131 and the refractory layer 133 of white corundum castable, the inner wall of the furnace body 131 is formed by stacking carbon bricks and refractory stones, electrode piles 136 are disposed on the furnace bottom 135, the number of the electrode piles 136 corresponds to that of the electrodes 132, each electrode pile 136 is located under each electrode 132, the electrodes 132 and the electrode piles 136 cooperate to carry out slag washing smelting on a first crushed material in the furnace body 131 to obtain raw material silicon, a slag flowing channel 137 is formed in the middle of the furnace body 131, slag liquid flows out in a high temperature area above a silicon slag interface in the furnace body 131 by using the slag flowing channel 137, and quantitative slag flowing and slag blocking are realized by blocking the slag flowing channel 137. The lower part of the furnace body 131 is provided with a silicon liquid outflow channel 138 for discharging silicon liquid. The specific process of slag washing smelting the first crushed material in the furnace body 131 by matching the electrode 132 with the electrode pile 136 to obtain raw material silicon is as follows: mixing the first crushed material and the silicon slag according to the mass ratio of 1:1 to obtain a silicon slag mixture; 200kg of silicon material is firstly filled below the electrode 132, after arc striking and melting, silicon slag mixture is quantitatively added, and smelting is carried out in a submerged arc smelting mode; when the mixture in the furnace body 131 is completely melted, the slag liquid is discharged through the slag flowing channel 137 in a high temperature state, then the slag is continuously added and melted, the slag liquid is continuously discharged, the slag washing operation of the first broken material is completed, and the raw material silicon is obtained.|[0017] The second crushing device 14 crushes the raw material silicon produced by the raw material silicon ore furnace 13 to obtain a second crushed material, the mesh number of which is 30-150 mesh.|[0018] The carbon removal device 15 calcines the second crushed material produced by the second crushing device 14 to reduce the carbon content in the second crushed material. Wherein, the carbon removing device 15 uses high-heating-value fuel and calcines the second crushed material in a reducing atmosphere, so that the carbon content in the calcined second crushed material is effectively reduced to below 0.4ppm.|[0019] Referring to fig. 3, the electron beam melting device 16 includes a control device 161, a charging device 162, a furnace body 163, two melting crucibles 164 arranged in the furnace body 163, a water-cooled copper crucible 165 and electron beam guns 166 correspondingly arranged above the melting crucibles and the water-cooled copper crucible, the control device 161 controls the charging device 162, the melting crucibles 164, the water-cooled copper crucible 165 and the electron beam guns 166 to work, the two melting crucibles 164 are arranged in parallel, the water-cooled copper crucible 165 is arranged below the two melting crucibles 164 and is positioned between the two melting crucibles 164, the charging device 162 is arranged on the furnace body 163 so as to add a predetermined amount of calcined second crushed material into the two melting crucibles 164 under the control of the control device 161, the electron beam guns 166 above the two melting crucibles 164 are controlled to melt and dephosphorize the second crushed material in the two melting crucibles, the control device 161 controls the two melting crucibles to alternately flow into the water-cooled copper crucible 165, the electron beam guns 166 above the control the water-cooled copper crucible 165 to scan in an area changing surface scanning mode and ensure that the melted raw materials are not volatilized to flow into a molten pool between the two melting pools and a predetermined interface by the molten bath according to a predetermined power; the area-changing surface scanning mode is to adjust the frequency of expanding and shrinking the scanning surface of the electron beam, so that the scanned area in the water-cooled copper crucible 165 is continuously changed from large to small to realize the control of the moving speed and the crystallization speed of the melting zone; after the raw material in the water-cooled copper crucible 165 is full, the control device 161 controls the electron beam gun 166 above the water-cooled copper crucible 165 to reduce the power and concentrate impurities in the silicon ingot to the center of the top of the silicon ingot in a surface scanning mode with unchanged area and gradually reduce the power, the silicon ingot in the water-cooled copper crucible is cooled and then discharged, a semi-finished polysilicon product is obtained, and the bottom and top impurity enrichment areas of the semi-finished polysilicon product are sawed to obtain polysilicon. Wherein, the control device 161 controls the charging device 162 to charge the predetermined amount of calcined second crushed materials into the two melting crucibles 164, and the control device 161 controls the electron beam gun 166 above the two melting crucibles 164 to perform the specific process of melting and dephosphorizing the second crushed materials in the two melting crucibles 164, which is as follows: the control device 161 controls the charging device 162 to charge each time a unit amount of the second crushed material into each melting crucible 164, the control device 161 controls the electron beam gun 166 to melt the unit amount of the second crushed material according to a first preset power for a first preset time period, then the unit amount of the second crushed material is charged into the melting crucible 164, and controls the electron beam gun 166 to melt the unit amount of the second crushed material which is charged for the second time according to the first preset power for the first preset time period, until the control device 161 calculates that the amount of the second crushed material which is charged into the melting crucible 164 corresponds to the preset amount, and then the control device 161 controls the two melting crucibles 164 to flow molten raw materials into the water-cooled copper crucible 165 alternately, and the flow times of the two melting crucibles 164 differ by a third preset time period. For example, in a preferred embodiment, the predetermined amount is 24kg, the unit amount of silicon material is 2kg, the first predetermined power is 300KW, the first predetermined period of time is 2 minutes, the second predetermined period of time is 6 minutes, and the third predetermined period of time is 15 minutes; the thickness of the molten pool is 3-5 cm. After the raw material in the water-cooled copper crucible 165 is filled, the control device 161 controls the electron beam gun 166 above the water-cooled copper crucible 165 to reduce the power and concentrate impurities in the silicon ingot to the top center of the silicon ingot by a surface scanning mode with a constant area and gradually reducing the power, and when the control device 161 controls the electron beam gun 166 above the water-cooled copper crucible 165 to gradually reduce the power until the power is reduced to 5kw and the scanning area of the surface scanning mode is a circle with a diameter of 10 cm.|[0020] In the crystalline silicon purification integrated system, the first crushing device crushes crude silicon materials to 30-150 meshes to obtain first crushed materials, the acid pickling device performs acid pickling on the first crushed materials produced by the first crushing device to remove impurities on the surfaces of the first crushed materials, the raw material silicon ore smelting furnace adopts a submerged arc smelting mode to perform slag washing, smelting and acid pickling on the first crushed materials subjected to impurity removal by the acid pickling device to obtain raw material silicon, the second crushing device crushes the raw material silicon produced by the raw material silicon ore smelting furnace to obtain second crushed materials with the mesh number of 30-150 meshes, the carbon removing device performs calcination on the second crushed materials produced by the second crushing device to reduce the carbon content in the second crushed materials, the control device of the electron beam smelting device controls the electron beam guns above the two smelting crucibles to perform smelting dephosphorization on the second crushed materials in the two smelting crucibles and controls the two smelting crucibles to alternately flow the molten raw materials into the water-cooled copper crucible successively, the control device of the electron beam smelting device controls the electron beam gun above the water-cooled copper crucible to scan and heat the raw material flowing into the water-cooled copper crucible in a surface scanning mode with area change and according to a first preset power, so as to ensure that a molten pool with preset thickness exists in the water-cooled copper crucible, impurities are continuously collected and volatilized into the molten pool by utilizing a solid-liquid interface between the molten pool and crystallized materials, after the raw material in the water-cooled copper crucible is full, the control device controls the electron beam gun above the water-cooled copper crucible to scan in a surface scanning mode with area unchanged and gradually reduce power, so as to reduce power and concentrate impurities in a silicon ingot to the center of the top of the silicon ingot, after the water-cooled copper crucible is cooled, the ingot is discharged to obtain a semi-finished polysilicon product, the bottom and the top impurity enrichment area of the semi-finished polysilicon product is sawed, to obtain polysilicon. Compared with the existing polysilicon production system, the invention has the following technical effects: 1. the crystalline silicon purification integrated system provided by the invention effectively solves the problem that each link of the whole process can be directly cut into due to the difference of raw material quality, and the purpose of high-efficiency production is realized; 2. the crystalline silicon purification integrated system provided by the invention effectively improves the yield of each main production link; 3. solves the requirement of special industrial silicon in the background technology and fully solves the problem of difficult source of raw materials; 4. the invention effectively improves the production efficiency of polysilicon by the hot slag washing smelting of the raw material silicon ore in the crystalline silicon purification integrated system, and solves the problems of small crucible volume, short service life and low yield per furnace in the intermediate frequency smelting in the background technology; 5. the crystalline silicon purification integrated system provided by the invention eliminates the use of ingot furnace directional solidification purification, and saves equipment investment; 6. according to the crystalline silicon purification integrated system, an electron beam zone melting technology is utilized, so that a link of removing metal impurities by utilizing an ingot furnace in the background technology is eliminated, the phosphorus removal index reaches the quality requirement (P is less than or equal to 0.1 ppm), the metal impurity removal rate reaches more than 99%, namely, 4N grade silicon material can be purified to 6N grade silicon material, meanwhile, the process time is greatly shortened, the energy consumption is effectively reduced, the smelting time is reduced from 30 hours to 8 hours, and the comprehensive electricity consumption is reduced from 25kwh/kg to 10kwh/kg;7. the quality of the product produced by the crystalline silicon purification integrated system provided by the invention is detected, and the quality meets the requirement of solar-grade polycrystalline silicon of the high-efficiency battery; 8. the crystalline silicon purification integrated system provided by the invention can control the production ton cost of polysilicon below 7 ten thousand yuan, and the power consumption of ton polysilicon is as low as within 4 ten thousand degrees. (CN107089665)|TECHNICAL FIELD|[0001] The invention relates to the technical field of polysilicon production, in particular to a crystalline silicon purification integrated system.|BACKGROUND ART|[0002] Since human beings enter the new century, photovoltaic power generation has been rapidly developed, photovoltaic power generation equipment prepared by taking crystalline silicon as a raw material is widely used, crystalline silicon photovoltaic maintains the mainstream position of solar photovoltaic power generation in a quite long time, the main raw material of the crystalline silicon photovoltaic power generation is solar grade polycrystalline silicon, along with the rapid development of the photovoltaic power generation, the preparation of the polycrystalline silicon is more and more highly required in the aspects of quality, energy consumption, environment, cost and the like, and the aim is to continuously adapt to the requirements of photovoltaic power generation on low price surfing.|[0003] The method for preparing solar grade polysilicon mainly comprises an improved Siemens method (chemical method), a silane method (chemical method), a metallurgical method and the like. The improved Siemens method occupies the market of absolute share, but the cost is about 120 yuan/kg, and the difficulty in reduction is still larger.|[0004] The existing technology for purifying and integrating solar-grade polysilicon prepared by a metallurgical method has the advantages of better quality, lower energy consumption and environmental friendliness, but the comprehensive cost is still higher, and the market share of the product is very small. The existing process route is as follows: specially-produced industrial silicon, simple directional solidification, hydrometallurgy I, slag washing refining, simple directional solidification, hydrometallurgy II, vacuum directional solidification, primary finishing, electron beam smelting and secondary finishing. The technical indexes are as follows: less than or equal to 0.1ppm of B, less than or equal to 0.1ppm of P, less than or equal to 0.1ppm of metal impurities, less than or equal to 0.4ppm of C, less than or equal to 1ppm of O, and resistivity: 0.8-3.0 Ω CM, minority carrier lifetime: more than or equal to 3 mu s, the photoelectric conversion efficiency is more than or equal to 17.5 percent, and the comprehensive power consumption is as follows: 58kwh/kg, direct production cost: 138 yuan/kg.|[0005] The above-mentioned prior art has the technical problems of longer process route, higher energy consumption and higher production cost, for example: the requirements on raw materials are high, and special industrial silicon needs to be produced, so that the quality requirements on silica, petroleum coke and the like are high; the high temperature required for removing boron causes high requirements on crucible materials, small crucible volume, short service life and low yield per furnace; the ingot furnace is utilized for directional solidification and purification, so that the time is long, the energy consumption is high, the investment is large, and the yield is low; the electron beam dephosphorization process has long design time and high energy consumption.|DISCLOSURE|Disclosure of Invention|[0006] In view of the foregoing, it is desirable to provide a crystalline silicon purification integrated system that has a short process route and reduced energy consumption and production costs.|[0007] A crystalline silicon purification integrated system comprising: the device comprises a first crushing device, an acid washing device, a raw material silicon ore heating furnace, a second crushing device, a carbon removal device and an electron beam smelting device; the first crushing device crushes the crude silicon material to 30 to 150 meshes to obtain a first crushed material. The acid washing device carries out acid washing on the first crushed material produced by the first crushing device so as to remove impurities on the surface of the first crushed material. The raw material silicon ore heating furnace adopts a submerged arc smelting mode to carry out the first crushed material after the slag washing smelting pickling device is used for pickling and removing impurities so as to obtain raw material silicon. The second crushing device crushes the raw material silicon produced by the raw material silicon ore heating furnace to obtain a second crushed material, and the mesh number of the second crushed material is 30-150 meshes. The carbon removing device calcines the second crushed material produced by the second crushing device to reduce the carbon content in the second crushed material, wherein the carbon content in the calcined second crushed material is less than 0.4ppm. The electron beam smelting device comprises a control device, a feeding device, a furnace body, two smelting crucibles arranged in the furnace body, a water-cooling copper crucible and electron beam guns correspondingly arranged above the smelting crucibles and the water-cooling copper crucible, wherein the control device controls the feeding device, the smelting crucibles, the water-cooling copper crucible and the electron beam guns to work; the area-changing surface scanning mode is to adjust the frequency of expanding and shrinking the scanning surface of the electron beam, so that the scanned area in the water-cooled copper crucible is continuously changed from large to small to realize the control of the moving speed and the crystallization speed of the melting zone; after the raw materials in the water-cooled copper crucible are full, the control device controls the electron beam gun above the water-cooled copper crucible to reduce the power and concentrate impurities in the silicon ingot to the center of the top of the silicon ingot in a surface scanning mode with unchanged area and gradually reduce the power, the silicon ingot in the water-cooled copper crucible is cooled and then is discharged to obtain a semi-finished polysilicon product, and the bottom and top impurity enrichment areas of the semi-finished polysilicon product are sawed to obtain polysilicon; wherein, the control device controls the charging device to add the second crushed material after the calcination of predetermined amount into two smelting crucibles, and the control device controls the electron beam gun above two smelting crucibles to smelt the specific process of dephosphorization to the second crushed material in two smelting crucibles: the control device controls the feeding device to feed a unit amount of second crushed material into each smelting crucible each time, controls the electron beam gun to smelt the unit amount of second crushed material according to the first preset power for a first preset time period, then feeds the unit amount of second crushed material into the smelting crucible and controls the electron beam gun to smelt the unit amount of second crushed material fed into the smelting crucible for the first preset time period according to the first preset power, until the control device calculates that the amount of the second crushed material fed into the smelting crucible corresponds to the preset amount, and then smelts the second preset time period, and then controls the two smelting crucibles to flow molten raw materials into the water-cooled copper crucible alternately, and the time difference of the two smelting crucible flows is a third preset time period.|[0008] In the crystalline silicon purification integrated system, the first crushing device crushes crude silicon materials to 30-150 meshes to obtain first crushed materials, the acid pickling device performs acid pickling on the first crushed materials produced by the first crushing device to remove impurities on the surfaces of the first crushed materials, the raw material silicon ore heating furnace adopts a submerged arc smelting mode to perform slag washing smelting and acid pickling on the first crushed materials subjected to impurity removal by the acid pickling device to obtain raw material silicon, the second crushing device crushes the raw material silicon produced by the raw material silicon ore heating furnace to obtain second crushed materials, the mesh number of the second crushed materials is 30-150 meshes, the carbon removal device calcines the second crushed materials produced by the second crushing device to reduce the carbon content in the second crushed materials, the control device of the electron beam gun of the electron beam smelting device controls the second crushed materials in the two smelting crucibles to perform phosphorus removal and controls the two smelting crucibles to alternately flow into the water-cooled copper crucible, the control device controls the electron beam gun above the electron beam gun of the electron beam smelting device to control the water-cooled copper crucible to scan in a surface changing area mode, the power of the water-cooled copper ingot is controlled to be concentrated to the top of a polycrystalline silicon ingot, the silicon ingot is concentrated in a water-cooled area is ensured to be concentrated by the water-cooled silicon ingot, and the water-cooled silicon ingot is concentrated in the top of the water-cooled crucible is not controlled to be concentrated to be in the water-cooled silicon ingot after the top surface is concentrated to be concentrated with the water-cooled silicon ingot is in the water-cooled silicon ingot is concentrated by the water-cooled surface area, and the silicon impurity is concentrated down to be concentrated down to the silicon impurity is concentrated down to the silicon solution in the silicon crucible is concentrated down to the silicon crucible, to obtain polysilicon. And further solves the technical problems of longer process route, higher energy consumption and higher production cost in the prior art.|DRAWINGS DESCRIPTION|[0009] FIG. 1 is a schematic diagram showing the connection of functional blocks of a crystalline silicon purification integrated system according to a preferred embodiment.|[0010] Fig. 2 is a schematic structural view of the raw material silicon ore furnace of fig. 1.|[0011] Fig. 3 is a schematic diagram illustrating connection of functional modules of the electron beam melting apparatus of fig. 1.|[0012] In the figure: the integrated system 10 for purifying crystalline silicon comprises a first crushing device 11, a pickling device 12, a raw material silicon ore smelting furnace 13, a furnace body 131, an electrode 132, a refractory layer 133 of white corundum castable, an electrode paste layer 134, a furnace bottom 135, an electrode pile 136, a slag flow channel 137, a silicon liquid outflow channel 138, a second crushing device 14, a carbon removing device 15, an electron beam smelting device 16, a control device 161, a feeding device 162, a furnace body 163, a smelting crucible 164, a water-cooled copper crucible 165 and an electron beam gun 166.|INVENTION MODE|Detailed Description|[0013] Referring to fig. 1, the integrated system 10 for purifying crystalline silicon includes a first crushing device 11, an acid washing device 12, a raw silicon ore furnace 13, a second crushing device 14, a decarbonizing device 15, and an electron beam melting device 16.|[0014] The first crushing device 11 crushes the crude silicon material to 30 to 150 mesh to obtain a first crushed material. Coarse silicon materials are defined as 553 industrial silicon as well as silicon scrap, that is to say various silicon materials with a purity of more than 99%.|[0015] The acid washing device 12 washes the first crushed material produced by the first crushing device 11 to remove impurities on the surface of the first crushed material. Further, the pickling device 12 performs pickling on the polysilicon which is produced by the electron beam melting device 16 and is subjected to impurity removal by a saw.|[0016] The raw material silicon ore furnace 13 performs slag washing, smelting and pickling of the first crushed material after pickling and impurity removal of the pickling device 12 in a submerged arc smelting manner to obtain raw material silicon. Referring to fig. 2, the raw material silicon ore smelting furnace 13 includes a furnace body 131, electrodes 132, a refractory layer 133 of white corundum castable disposed on an inner wall of the furnace body 131, an electrode paste layer 134 and a furnace bottom 135 made of electrode paste, wherein the electrode paste layer 134 is disposed between the inner wall of the furnace body 131 and the refractory layer 133 of white corundum castable, the inner wall of the furnace body 131 is formed by stacking carbon bricks and refractory stones, electrode piles 136 are disposed on the furnace bottom 135, the number of the electrode piles 136 corresponds to that of the electrodes 132, each electrode pile 136 is located under each electrode 132, the electrodes 132 and the electrode piles 136 cooperate to carry out slag washing smelting on a first crushed material in the furnace body 131 to obtain raw material silicon, a slag flowing channel 137 is formed in the middle of the furnace body 131, slag liquid flows out in a high temperature area above a silicon slag interface in the furnace body 131 by using the slag flowing channel 137, and quantitative slag flowing and slag blocking are realized by blocking the slag flowing channel 137. The lower part of the furnace body 131 is provided with a silicon liquid outflow channel 138 for discharging silicon liquid. The specific process of slag washing smelting the first crushed material in the furnace body 131 by matching the electrode 132 with the electrode pile 136 to obtain raw material silicon is as follows: mixing the first crushed material and the silicon slag according to the mass ratio of 1:1 to obtain a silicon slag mixture; 200kg of silicon material is firstly filled below the electrode 132, after arc striking and melting, silicon slag mixture is quantitatively added, and smelting is carried out in a submerged arc smelting mode; when the mixture in the furnace body 131 is completely melted, the slag liquid is discharged through the slag flowing channel 137 in a high temperature state, then the slag is continuously added and melted, the slag liquid is continuously discharged, the slag washing operation of the first broken material is completed, and the raw material silicon is obtained.|[0017] The second crushing device 14 crushes the raw material silicon produced by the raw material silicon ore furnace 13 to obtain a second crushed material, the mesh number of which is 30-150 mesh.|[0018] The carbon removal device 15 calcines the second crushed material produced by the second crushing device 14 to reduce the carbon content in the second crushed material. Wherein, the carbon removing device 15 uses high-heating-value fuel and calcines the second crushed material in a reducing atmosphere, so that the carbon content in the calcined second crushed material is effectively reduced to below 0.4ppm.|[0019] Referring to fig. 3, the electron beam melting device 16 includes a control device 161, a charging device 162, a furnace body 163, two melting crucibles 164 arranged in the furnace body 163, a water-cooled copper crucible 165 and electron beam guns 166 correspondingly arranged above the melting crucibles and the water-cooled copper crucible, the control device 161 controls the charging device 162, the melting crucibles 164, the water-cooled copper crucible 165 and the electron beam guns 166 to work, the two melting crucibles 164 are arranged in parallel, the water-cooled copper crucible 165 is arranged below the two melting crucibles 164 and is positioned between the two melting crucibles 164, the charging device 162 is arranged on the furnace body 163 so as to add a predetermined amount of calcined second crushed material into the two melting crucibles 164 under the control of the control device 161, the electron beam guns 166 above the two melting crucibles 164 are controlled to melt and dephosphorize the second crushed material in the two melting crucibles, the control device 161 controls the two melting crucibles to alternately flow into the water-cooled copper crucible 165, the electron beam guns 166 above the control the water-cooled copper crucible 165 to scan in an area changing surface scanning mode and ensure that the melted raw materials are not volatilized to flow into a molten pool between the two melting pools and a predetermined interface by the molten bath according to a predetermined power; the area-changing surface scanning mode is to adjust the frequency of expanding and shrinking the scanning surface of the electron beam, so that the scanned area in the water-cooled copper crucible 165 is continuously changed from large to small to realize the control of the moving speed and the crystallization speed of the melting zone; after the raw material in the water-cooled copper crucible 165 is full, the control device 161 controls the electron beam gun 166 above the water-cooled copper crucible 165 to reduce the power and concentrate impurities in the silicon ingot to the center of the top of the silicon ingot in a surface scanning mode with unchanged area and gradually reduce the power, the silicon ingot in the water-cooled copper crucible is cooled and then discharged, a semi-finished polysilicon product is obtained, and the bottom and top impurity enrichment areas of the semi-finished polysilicon product are sawed to obtain polysilicon. Wherein, the control device 161 controls the charging device 162 to charge the predetermined amount of calcined second crushed materials into the two melting crucibles 164, and the control device 161 controls the electron beam gun 166 above the two melting crucibles 164 to perform the specific process of melting and dephosphorizing the second crushed materials in the two melting crucibles 164, which is as follows: the control device 161 controls the charging device 162 to charge each time a unit amount of the second crushed material into each melting crucible 164, the control device 161 controls the electron beam gun 166 to melt the unit amount of the second crushed material according to a first preset power for a first preset time period, then the unit amount of the second crushed material is charged into the melting crucible 164, and controls the electron beam gun 166 to melt the unit amount of the second crushed material which is charged for the second time according to the first preset power for the first preset time period, until the control device 161 calculates that the amount of the second crushed material which is charged into the melting crucible 164 corresponds to the preset amount, and then the control device 161 controls the two melting crucibles 164 to flow molten raw materials into the water-cooled copper crucible 165 alternately, and the flow times of the two melting crucibles 164 differ by a third preset time period. For example, in a preferred embodiment, the predetermined amount is 24kg, the unit amount of silicon material is 2kg, the first predetermined power is 300KW, the first predetermined period of time is 2 minutes, the second predetermined period of time is 6 minutes, and the third predetermined period of time is 15 minutes; the thickness of the molten pool is 3-5 cm. After the raw material in the water-cooled copper crucible 165 is filled, the control device 161 controls the electron beam gun 166 above the water-cooled copper crucible 165 to reduce the power and concentrate impurities in the silicon ingot to the top center of the silicon ingot by a surface scanning mode with a constant area and gradually reducing the power, and when the control device 161 controls the electron beam gun 166 above the water-cooled copper crucible 165 to gradually reduce the power until the power is reduced to 5kw and the scanning area of the surface scanning mode is a circle with a diameter of 10 cm.|[0020] In the crystalline silicon purification integrated system, the first crushing device crushes crude silicon materials to 30-150 meshes to obtain first crushed materials, the acid pickling device performs acid pickling on the first crushed materials produced by the first crushing device to remove impurities on the surfaces of the first crushed materials, the raw material silicon ore smelting furnace adopts a submerged arc smelting mode to perform slag washing, smelting and acid pickling on the first crushed materials subjected to impurity removal by the acid pickling device to obtain raw material silicon, the second crushing device crushes the raw material silicon produced by the raw material silicon ore smelting furnace to obtain second crushed materials with the mesh number of 30-150 meshes, the carbon removing device performs calcination on the second crushed materials produced by the second crushing device to reduce the carbon content in the second crushed materials, the control device of the electron beam smelting device controls the electron beam guns above the two smelting crucibles to perform smelting dephosphorization on the second crushed materials in the two smelting crucibles and controls the two smelting crucibles to alternately flow the molten raw materials into the water-cooled copper crucible successively, the control device of the electron beam smelting device controls the electron beam gun above the water-cooled copper crucible to scan and heat the raw material flowing into the water-cooled copper crucible in a surface scanning mode with area change and according to a first preset power, so as to ensure that a molten pool with preset thickness exists in the water-cooled copper crucible, impurities are continuously collected and volatilized into the molten pool by utilizing a solid-liquid interface between the molten pool and crystallized materials, after the raw material in the water-cooled copper crucible is full, the control device controls the electron beam gun above the water-cooled copper crucible to scan in a surface scanning mode with area unchanged and gradually reduce power, so as to reduce power and concentrate impurities in a silicon ingot to the center of the top of the silicon ingot, after the water-cooled copper crucible is cooled, the ingot is discharged to obtain a semi-finished polysilicon product, the bottom and the top impurity enrichment area of the semi-finished polysilicon product is sawed, to obtain polysilicon. Compared with the existing polysilicon production system, the invention has the following technical effects: 1. the crystalline silicon purification integrated system provided by the invention effectively solves the problem that each link of the whole process can be directly cut into due to the difference of raw material quality, and the purpose of high-efficiency production is realized; 2. the crystalline silicon purification integrated system provided by the invention effectively improves the yield of each main production link; 3. solves the requirement of special industrial silicon in the background technology and fully solves the problem of difficult source of raw materials; 4. the invention effectively improves the production efficiency of polysilicon by the hot slag washing smelting of the raw material silicon ore in the crystalline silicon purification integrated system, and solves the problems of small crucible volume, short service life and low yield per furnace in the intermediate frequency smelting in the background technology; 5. the crystalline silicon purification integrated system provided by the invention eliminates the use of ingot furnace directional solidification purification, and saves equipment investment; 6. according to the crystalline silicon purification integrated system, an electron beam zone melting technology is utilized, so that a link of removing metal impurities by utilizing an ingot furnace in the background technology is eliminated, the phosphorus removal index reaches the quality requirement (P is less than or equal to 0.1 ppm), the metal impurity removal rate reaches more than 99%, namely, 4N grade silicon material can be purified to 6N grade silicon material, meanwhile, the process time is greatly shortened, the energy consumption is effectively reduced, the smelting time is reduced from 30 hours to 8 hours, and the comprehensive electricity consumption is reduced from 25kwh/kg to 10kwh/kg;7. the quality of the product produced by the crystalline silicon purification integrated system provided by the invention is detected, and the quality meets the requirement of solar-grade polycrystalline silicon of the high-efficiency battery; 8. the crystalline silicon purification integrated system provided by the invention can control the production ton cost of polysilicon below 7 ten thousand yuan, and the power consumption of ton polysilicon is as low as within 4 ten thousand degrees. Family Number|(77100625)|77100625|Abstract|(CN107089665B B)|The invention discloses a crystalline silicon purification integrated system which comprises a first crushing device , a pickling device , a raw silicon ore smelting electric furnace , a second crushing device , a carbon removal device and an electron - beam smelting device . Crude silicon is crushed by the first crushing device , and the crushed material is pickled by the pickling device and then subjected to wash heat smelting by utilizing the raw silicon ore smelting electric furnace so as to obtain the raw silicon . After the raw silicon is crushed by the second crushing device , the raw silicon is calcined by the carbon removal device so as to reduce the carbon content in the crushed material produced by the second crushing device , the calcined crushed material is subjected to smelting phosphorous removal by the electron - beam smelting device , the raw materials subjected to phosphorous removal are scanned and heated in an area - variable surface scanning manner and according to a first preset power , and then the impurities are continuously gathered and volatilized into a molten bath by utilizing a solid - liquid interface between the molten bath and the crystallized materials . An electron beam gun is controlled to obtain semi - finished polycrystalline silicon in the area - variable surface scanning manner and at gradually decreased power , and the bottom and top impurity enrichment areas of the semi - finished polycrystalline silicon are sawed so as to obtain the polycrystalline silicon . |CPC codes|(CN107089665B B)|C01B - 033/037 |IPC codes|(CN107089665B B)|C01B - 033/037 | Materials, metallurgy|Surface technology, coating C01B-033/037|C30B-028/06|C30B-029/06 C01B-033/037|C30B-028/06|C30B-029/06 C01B-033/037|C30B-028/06|C30B-029/06 C01B-033/037|C30B-028/06|C30B-029/06 CN109023521 CN109023521 82531772 WHO=Examiner SELF=N CAT=A CN103588208|WO2012100485|CN101935041 CN103588208 61786844 WHO=Examiner SELF=N|WO2012100485 7357781 WHO=Examiner SELF=N|CN101935041 7170734 WHO=Examiner SELF=N CN101935041; CN103588208; WO2012100485 GRANTED (CN107089665)|GRANTED ALIVE (CN107089665)|ALIVE (CN107089665)|LEGAL DETAILS FOR CN107089665|Actual or expected expiration date=2037-05-25|Legal state=ALIVE|Status=GRANTED|Event publication date=2017-05-25|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201710377733|Application date=2017-05-25|Standardized application number=2017CN-0377733|Event publication date=2017-08-25|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN107089665|Publication stage code=A|Publication date=2017-08-25|Standardized publication number=CN107089665|Event publication date=2017-08-25|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2017-09-19|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-05-16|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN107089665|Publication stage code=B|Publication date=2023-05-16|Standardized publication number=CN107089665B|Event publication date=2023-05-16|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2025-10-14|Event code=CN/PP01|Event indicator=Pos|Event group=Restitution or restoration Opposition and reexamination events|Preservation and discharge of patent right|Effective date of the event=2025-09-16 (CN107089665)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjklwi/R7i8juxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067791183&ekey=2136&xpn=CN107089665B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=Dsz2nZpKv0P2eMJzC6JSQLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN107089665)|CN (CN107089665)|NAME=NINGXIA DONGMENG ENERGY CO LTD , COUNTRY=CN (CN107089665)|NAME=SUN YANHU;NINGXIA SANYUANXIN INTELLECTUAL PROPERTY AGENCY FIRM (GENERAL PARTNERSHIP) , REG=64105|(CN107089665)|NAME=SUN YANHU;NINGXIA HETIAN LAW FIRM (CN107089665)|NAME=LIU YINGKUAN|NAME=WEN WEIDONG|NAME=FENG QUANYI|NAME=ZHOU XUEMEI|NAME=YANG QI|NAME=LU ZANDONG|NAME=YAN GANG|NAME=LI YANG|NAME=JIANG LIHUA|NAME=SUO XIAOFENG|(CN107089665)|NAME=LIU YINGKUAN|NAME=WEN WEIDONG|NAME=FENG QUANYI|NAME=ZHOU XUEMEI|NAME=YANG QI|NAME=LU ZANDONG|NAME=YAN GANG|NAME=LI YANG|NAME=JIANG LIHUA|NAME=SUO XIAOFENG 0 1 Titre: (CN107089665)|Crystalline silicon purification integrated system Résumé: (CN107089665)|The invention discloses a crystalline silicon purification integrated system which comprises a first crushing device, a pickling device, a raw silicon ore smelting electric furnace, a second crushing device, a carbon removal device and an electron-beam smelting device. Crude silicon is crushed by the first crushing device, and the crushed material is pickled by the pickling device and then subjected to wash heat smelting by utilizing the raw silicon ore smelting electric furnace so as to obtain the raw silicon. After the raw silicon is crushed by the second crushing device, the raw silicon is calcined by the carbon removal device so as to reduce the carbon content in the crushed material produced by the second crushing device, the calcined crushed material is subjected to smelting phosphorous removal by the electron-beam smelting device, the raw materials subjected to phosphorous removal are scanned and heated in an area-variable surface scanning manner and according to a first preset power, and then the impurities are continuously gathered and volatilized into a molten bath by utilizing a solid-liquid interface between the molten bath and the crystallized materials. An electron beam gun is controlled to obtain semi-finished polycrystalline silicon in the area-variable surface scanning manner and at gradually decreased power, and the bottom and top impurity enrichment areas of the semi-finished polycrystalline silicon are sawed so as to obtain the polycrystalline silicon. 78 Abstract gpt-4o-mini no The article focuses on a crystalline silicon purification system and does not mention accelerated weathering, CO₂ capture, or related processes.
86 CN202511056627 CN202511056627 CN120548812|CN120548812 115835752 CN120548812 B 2025-10-03 [CN120548812B]|CN120548812 A 2025-08-29 [CN120548812] 2025-07-30 2025-07-30 2025-10-03|2025-08-29 (CN120548812B)|2025-10-03 (CN120548812)|2045-07-30 (CN120548812)|Rice field soil carburetion and capacity expansion method based on biochar-based organic fertilizer (CN120548812)|The invention relates to the technical field of soil function improvement, in particular to a rice field soil recarburization and capacity expansion method based on a charcoal-based organic fertilizer. The method comprises the following steps: crushing a biomass raw material, pyrolyzing and cooling to obtain biochar; immersing the biochar in a functional bacteria solution containing actinomycetes and bacillus for activating treatment to obtain modified biochar; mixing the modified biochar and decomposed straw, composting and fermenting to obtain organic fertilizers with different particle sizes; the large-particle-size organic fertilizer is applied to deep soil, the soil is covered with soil after straw is laid on the soil, and the small-particle-size organic fertilizer is applied to surface soil. Through layered application, the large-particle-size biochar repairs the deep soil structure and expands the carbon storage capacity, and meanwhile, the carbon stability is improved through carbon-nitrogen synergistic metabolism driven by functional bacteria, so that the carbon immobilization efficiency is improved, meanwhile, soil recarburization and expansion are achieved, the contradiction between carbon sequestration and structure degradation and nutrient imbalance in a traditional recarburization and expansion technology is solved, and the soil recarburization and expansion efficiency is improved. Synergic improvement of a carbon sink function and agricultural productivity is promoted. NORTHEAST INSTITUTE OF GEOGRAPHY & AGROECOLOGY - CHINESE ACADEMY OF SCIENCES (CN120548812)|NORTHEAST INSTITUTE OF GEOGRAPHY & AGROECOLOGY CHINESE ACADEMY OF SCIENCES ([CN])|(CN120548812)|NORTHEAST INSTITUTE OF GEOGRAPHY & AGROECOLOGY CHINESE ACADEMY OF SCIENCES ([CN]) WANG WEIQI|ZHANG HAO|ZOU YUANCHUN|LIANG YAO|LIANG SHUANG (CN120548812)|WANG WEIQI|ZHANG HAO|ZOU YUANCHUN|LIANG YAO|LIANG SHUANG|(CN120548812)|WANG WEIQI|ZHANG HAO|ZOU YUANCHUN|LIANG YAO|LIANG SHUANG (CN120548812)|QIU YU;Shenyang Hongmai Intellectual Property Agency (General Partnership)|Reg. Nb: 21274 (CN120548812)|It is not necessary here nor is it exhaustive of all embodiments.|However, the traditional technology generally applies organic fertilizer or biochar to surface layer or shallow soil uniformly, microorganisms in deep soil are led by anaerobic bacteria due to lack of oxygen, the decomposition capacity of the deep soil is obviously limited, the mineralization rate of organic carbon loaded by large-particle-size biochar is extremely low, carbon and nitrogen nutrients are retained in the deep layer for a long time, dislocation is formed with the requirement of a rice root system distribution area (0-20 cm surface layer), and the nutrient leaching risk is caused.|In the technical scheme, in the step 4, the proportion of the modified biochar, the decomposed straw compost and the edible fungus residues is (5-6) in percentage by mass, 1 is mixed uniformly until the uniformity is more than or equal to 95%, the water content of the materials is regulated to 50% -60%, the microbial activity is limited by the water content being lower than 50%, the anaerobic fermentation is caused by the water content being higher than 60%, the composting fermentation lasts for 5-7 days, the composting temperature is controlled to be between 55-65 ℃, the degradation of cellulose by thermophilic bacteria is promoted, functional bacteria are inactivated by the excessive temperature of the composting body, and the composting heat dissipation is needed.|In view of the technical problems that in the prior art, the traditional soil carburetion technology has low carbon holding efficiency, aggravated acidification and hardening and mismatch of carbon and nitrogen nutrient supply and demand of deep soil due to a single application strategy, and has negative influence.| (CN120548812)|1. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer is characterized by comprising the following steps of: Step 1, crushing a biomass raw material, pyrolyzing the biomass raw material at 500-700 ℃ for 5-8 hours, and cooling the biomass raw material to obtain biochar; step 2, preparing functional bacterial liquid containing actinomycetes and bacillus according to the part ratio of (1-3): 1, wherein the number of viable bacteria of the functional bacterial liquid ;Step 3, immersing the biochar in the functional bacterial liquid for activation treatment, and controlling the volume ratio of the functional bacterial liquid to the biochar to be 1 (2-3) to obtain modified biochar; Step 4, mixing the modified biochar with the decomposed straw, composting and fermenting, granulating and screening after the completion of the composting to obtain organic fertilizers with different particle sizes; step 5, applying organic fertilizer with large grain size into deep soil, paving pretreated straw on the soil, covering the soil, and applying organic fertilizer with small grain size into surface soil; in the step 3, the environment temperature of the activation treatment is controlled to be 25-30 ℃, the activation treatment is carried out for 18-24 hours at the constant temperature of 25-30 ℃, and the modified biochar is dehydrated until the water content is 5-10%. | (CN120548812)|The application provides a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer, which comprises the following steps:|The application relates to the technical field of soil function improvement, in particular to a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer.|The invention relates to the technical field of soil function improvement, in particular to a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer.| (CN120548812)|ION(100,19)|BIOCHAR ORGANIC FERTILIZER(100,16)|RICE FIELD SOIL(100,16)|CAPACITY EXPANSION(100,4)|PAVING PRETREATED STRAW(62,5)|DECOMPOSED STRAW COMPOST(61,4)|DILATION(56,15)|COMPOSTING FERMENTATION LAST(47,3)|STRAW DECOMPOSITION(46,15)|SOIL DEPTH(44,13)|THERMOPHILIC BACTERIA(43,1)|AGGRAVATED ACIDIFICATION(42,1)|ANAEROBIC FERMENTATION(42,1)|MODIFIED BIOCHAR(39,14)|ORGANIC FERTILIZER(38,51)|DEEP SOIL DECOMPOSITION CAPACITY(37,1)|FUNCTIONAL BACTERIAL LIQUID(36,13)|NUTRIENT LEACHING(36,2)|ACTIVATION TREATMENT(34,10)|NITROGEN NUTRIENT(34,2)|DECOMPOSED STRAW PRETREATMENT(33,4)|MODIFIED BIOCHAR PROPORTION(33,3)|VIABLE BACTERIA(32,2)|COMPOSTING COMPLETION(30,3)|EDIBLE FUNGUS RESIDUE(29,5)|CELLULOSE DEGRADATION(29,1)|REGULAR SPRINKLING IRRIGATION(28,3)|PAVING STRAW(28,1)|SHALLOW SOIL(28,1)|FUNCTIONAL BACTERIUM(27,5)|COMPOSITE MICROBIAL INOCULUM(26,3)|DECOMPOSITION CAPACITY(25,1)|NUTRIENT IMBALANCE(24,2)|CARBON NITROGEN COMETABOLISM(24,1)|CARBON MISMATCH(23,1)|BIOCHAR(22,21)|GROUND(22,17)|COMPOSTING(22,7)|BACILLUS SUBTILIS VIABLE COUNT(22,1)|COMPOSTING HEAT DISSIPATION(22,1)|MINERALIZATION(22,1)|ASPERGILLUS ORYZAE(21,5)|COMPOSTING TEMPERATURE(21,3)|GROUND COVER(19,1)|NEGATIVE INFLUENCE(19,1)|ACTINOMYCETE(18,12)|ORGANIC FERTILIZER APPLICATION(17,4)|PRETREATED STRAW LAYER(17,3)|DISLOCATION(17,1)|MESH SIEVE(17,1)|BIOMASS RAW MATERIAL(15,13)|BACILLUS(15,9)|ANAEROBIC BACTERIUM(15,2)|CARBON RESERVOIR CAPACITY(15,2)|ADDING STRAW(15,1)|DOSAGE(13,9)|FUNCTIONAL BACTERIUM LIQUID(13,4)|LIGNIN CONTENT(13,3)|STRUCTURAL DEGRADATION(13,3)|HECTARE(12,5)|MICROORGANISM(12,4)|HARDENING(12,2)|SOIL FUNCTION(12,2)|AGRICULTURAL PRODUCTIVITY(11,3)|DEEP SOIL STRUCTURE REPAIR(11,1)|PILE(11,1)|WATER CONTENT(10,16)|CELLULOSE DEGRADATION RATE(10,3)|ENVIRONMENT TEMPERATURE(10,3)|GROUND LAYER(9,4)|CRUSHED BIOMASS RAW MATERIAL(9,1)|DISTRIBUTION AREA(9,1)|ANAEROBIC FLORA METABOLIC ACTIVITY(8,2)|CRUSHING BIOMASS RAW MATERIAL(8,2)|PILING(8,2)|SYNERGISTIC CONTRADICTION(8,2)|DEEP ANAEROBIC METHANOGENESIS RISK(8,1)|DIFFERENTIATION STRATEGY LAYERING(8,1)|RICE ROOT SYSTEM(8,1)|PARTICLE SIZE(7,14)|CARBON NITROGEN RATIO(7,3)|CONSTANT TEMPERATURE(7,3)|ANTIHARDENING EXPERIMENT VERIFICATION(7,1)|BIOCHAR PARTICLE AGGLOMERATION(7,1)|SOIL ECOSYSTEM DEEP RESEARCH(7,1)|STRAW BRIDGE PRETREATMENT(7,1)|BIOMASS RAW MATERIAL PARTICLE(6,3)|COOL BIOMASS RAW MATERIAL(6,3)|EXTRACELLULAR ENZYME SECRETION(6,2)|HARDENING INHIBITION(6,2)|MICROBIAL DECOMPOSITION(6,2)|NUTRIENT UTILIZATION(6,2)|ACIDIFICATION INHIBITION ASSAY(6,1)|COMPOSTING HUMIFICATION(6,1)|FLORA DORMANCY(6,1)|NEUTRALIZATION TITRATIONCONCENTRATION(6,1)|GRAIN SIZE(5,22)|CARBON INCREMENT(5,3)|ORGANIC CARBON(5,3)|CARBON SINK FUNCTION(5,2)|FUNCTIONAL FLORA(5,2)|NUTRIENT REQUIREMENT(5,2)|REGULATION DIRECTION(5,2)|STRAW POWDER(5,2)|ACCELERATE MINERALIZATION(5,1)|AEROBIC FUNCTIONAL BACTERIUM(5,1)|BACILLUS METABOLITE(5,1)|BIOCHAR ADSORPTION CAPACITY(5,1)|BIOCHAR FERTILIZER(5,1)|BIOCHAR PORE(5,1)|BIOCHAR PROTECTION(5,1)|BIOCHAR WETTING(5,1)|CARBON SEQUESTRATION BIDIRECTIONAL OPTIMIZATION(5,1)|COVERING PRETREATED STRAW(5,1)|CULTIVATION DISTURBANCE(5,1)|DEEP SOIL ANAEROBIC ENVIRONMENT(5,1)|DEEP SOIL ANOXIC ENVIRONMENT(5,1)|EXTRACELLULAR POLYSACCHARIDE(5,1)|FUNGUS DREG(5,1)|HYDROLYZABLE ACIDTAKING(5,1)|HYPOXIA TOLERANT FUNCTIONAL BACTERIUM(5,1)|INCOMPLETE CARBONIZATION(5,1)|LAYERED FERTILIZATION(5,1)|MICROBIAL COLONIZATION(5,1)|MICROORGANISM ADHESION(5,1)|MICROORGANISM TOLERANCE(5,1)|MIXED BACTERIUM POLLUTION(5,1)|MOISTURE PERMEATION INTERACTION(5,1)|NPK FERTILIZER(5,1)|NUTRIENT SYNERGISTIC RELEASE(5,1)|PORE VENTILATION(5,1)|PYROLYSIS CARBONIZATION(5,1)|PYROLYSIS UNIFORMITY(5,1)|SMALL GRAIN ORGANIC FERTILIZER(5,1)|SOIL FERTILIZER RETAINING CAPACITY(5,1)|THERMOCHEMICAL DECOMPOSITION(5,1)|UNDISTURBED SOIL COLUMN(5,1)|DEEP LAYER(4,6)|VOLUME RATIO(4,4)|CELLULASE(4,3)|ALKALINE ENVIRONMENT(4,2)|BACILLUS AMYLOLIQUEFACIENS(4,2)|CARBON DECOMPOSITION(4,2)|CROP GROWTH(4,2)|LARGE GRAIN DIAMETER(4,2)|CRUSHING RICE STRAW(4,1)|DEEP NUTRIENT LOSS RISK(4,1)|DRY LAND SUBMERSION(4,1)|HARDENING RELIEF(4,1)|HOG MANURE(4,1)|HYPOXIA RESISTANT FUNCTIONAL BACTERIUM(4,1)|INSOLUBLE NUTRIENT(4,1)|MICROORGANISM LOADING(4,1)|NITROGEN COMETABOLISM(4,1)|QUICKLY RELEASING NUTRIENT(4,1)|RICE EARLY GROWTH(4,1)|SINGLE APPLICATION PROGRAM STRATEGY(4,1)|SOIL BORNE PATHOGENIC BACTERIUM(4,1)|VERIFYING EXPERIMENT(4,1)|WEED SEED(4,1)|SURFACE SOIL(3,12)|GRAIN SIZE BIOCHAR(3,7)|MASS RATIO(3,6)|LARGE PARTICLE SIZE BIOCHAR(3,3)|PART RATIO(3,3)|PYROLYSIS TIME(3,3)|SHORT SECTION(3,3)|DEEP SOIL AIR PERMEABILITY(3,2)|MICROPORE(3,2)|SLOW RELEASE BARRIER(3,2)|SUPERNATANT(3,2)|WATER CONDUCTION(3,2)|ADOPTING ORGANIC FERTILIZER(3,1)|AGGLOMERATE SEPARATION(3,1)|BALANCE NUTRIENT(3,1)|BIOCHAR PHYSICAL ADSORPTION CAPACITY(3,1)|BIOCHAR PYROLYSIS TEMPERATURE(3,1)|CLAY MINERAL(3,1)|COMPOSITE COLLOID(3,1)|DEEP SOIL CARBON MINERALIZATION(3,1)|GROUND MINERAL(3,1)|INERT NUTRIENT(3,1)|LAYER NUTRIENT COMPETITION(3,1)|NITROGEN COMPETITION(3,1)|NITROGEN MORPHOLOGY(3,1)|PHENOLIC HYDROXYL(3,1)|PORE ADSORPTION(3,1)|PROTECT MICROORGANISM(3,1)|PYROLYSIS BIOCHAR POROUS STRUCTURE(3,1)|SETTLING(3,1)|STRAW CELLULOSE(3,1)|VOLATILIZATION LOSS(3,1)|WET CARBON CAKING(3,1)|COOLING TIME(2,3)|ACIDIC ENVIRONMENT(2,1)|AMMONIA NITROGEN(2,1)|AMMONIA RELEASE(2,1)|APERTURE SIEVE(2,1)|ASH CONTENT(2,1)|BACTERIAL LIQUID VIABLE COUNT(2,1)|BASIC ASH(2,1)|DECARBOXYLATION(2,1)|DECOMPOSITION RESISTANCE(2,1)|DEEP CARBON STABILITY(2,1)|DEEP SOIL POROSITY(2,1)|DRY LAND MASS(2,1)|EXCHANGEABLE ACID(2,1)|EXTRACTION COLUMN(2,1)|FERTILIZER APPLICATION(2,1)|HUMUS FORMATION(2,1)|IMPLEMENTATION SITE(2,1)|ISTHE DROP(2,1)|LOW CARBON(2,1)|METHANOGENESIS PATH(2,1)|METHANOL WATER EXTRACTING(2,1)|MICROBIAL LOAD(2,1)|MICROENVIRONMENT(2,1)|MICROORGANISM FUNCTIONAL ACTIVITY PERIOD(2,1)|NEGATIVE LINKAGE(2,1)||(CN120548812)|ION(100,20)|BIOCHAR ORGANIC FERTILIZER(100,17)|RICE FIELD SOIL(100,17)|CAPACITY EXPANSION(100,4)|DECOMPOSED STRAW COMPOST(59,4)|DILATION(57,16)|COMPOSTING FERMENTATION LAST(46,3)|STRAW DECOMPOSITION(45,15)|SOIL DEPTH(43,13)|THERMOPHILIC BACTERIA(42,1)|AGGRAVATED ACIDIFICATION(41,1)|ANAEROBIC FERMENTATION(41,1)|ORGANIC FERTILIZER(40,53)|DEEP SOIL DECOMPOSITION CAPACITY(36,1)|MODIFIED BIOCHAR(35,14)|FUNCTIONAL BACTERIAL LIQUID(35,13)|NUTRIENT LEACHING(35,2)|DECOMPOSED STRAW PRETREATMENT(33,4)|NITROGEN NUTRIENT(33,2)|PAVING PRETREATED STRAW(32,4)|MODIFIED BIOCHAR PROPORTION(32,3)|PRETREATED STRAW(31,4)|VIABLE BACTERIA(31,2)|COMPOSTING COMPLETION(30,3)|EDIBLE FUNGUS RESIDUE(28,5)|CELLULOSE DEGRADATION(28,1)|PAVING STRAW(28,1)|REGULAR SPRINKLING IRRIGATION(27,3)|SHALLOW SOIL(27,1)|ACTIVATION TREATMENT(26,10)|FUNCTIONAL BACTERIUM(26,5)|COMPOSITE MICROBIAL INOCULUM(26,3)|DECOMPOSITION CAPACITY(24,1)|NUTRIENT IMBALANCE(23,2)|CARBON MISMATCH(23,1)|CARBON NITROGEN COMETABOLISM(23,1)|GROUND(22,17)|COMPOSTING(22,7)|COMPOSTING HEAT DISSIPATION(22,1)|BIOCHAR(21,21)|COMPOSTING TEMPERATURE(21,3)|MINERALIZATION(21,1)|GROUND COVER(18,1)|NEGATIVE INFLUENCE(18,1)|ACTINOMYCETE(17,12)|PRETREATED STRAW LAYER(17,3)|DISLOCATION(17,1)|MESH SIEVE(17,1)|BACILLUS(15,9)|CARBON RESERVOIR CAPACITY(15,2)|ADDING STRAW(15,1)|BIOMASS RAW MATERIAL(14,13)|ANAEROBIC BACTERIUM(14,2)|FUNCTIONAL BACTERIUM LIQUID(13,4)|STRUCTURAL DEGRADATION(13,3)|DOSAGE(12,9)|HECTARE(12,5)|MICROORGANISM(12,4)|LIGNIN CONTENT(12,3)|HARDENING(12,2)|SOIL FUNCTION(11,2)|DEEP SOIL STRUCTURE REPAIR(11,1)|ASPERGILLUS ORYZAE(10,4)|AGRICULTURAL PRODUCTIVITY(10,3)|CELLULOSE DEGRADATION RATE(10,3)|PILE(10,1)|WATER CONTENT(9,16)|BACILLUS SUBTILIS(9,4)|GROUND LAYER(9,4)|CRUSHED BIOMASS RAW MATERIAL(9,1)|DISTRIBUTION AREA(9,1)|ORGANIC FERTILIZER APPLICATION(8,3)|ANAEROBIC FLORA METABOLIC ACTIVITY(8,2)|CRUSHING BIOMASS RAW MATERIAL(8,2)|PILING(8,2)|SYNERGISTIC CONTRADICTION(8,2)|DIFFERENTIATION STRATEGY LAYERING(8,1)|RICE ROOT SYSTEM(8,1)|PARTICLE SIZE(7,14)|CARBON NITROGEN RATIO(7,3)|ANTIHARDENING EXPERIMENT VERIFICATION(7,1)|BIOCHAR PARTICLE AGGLOMERATION(7,1)|DEEP ANAEROBIC METHANOGENESIS RISK(7,1)|SOIL ECOSYSTEM DEEP RESEARCH(7,1)|STRAW BRIDGE PRETREATMENT(7,1)|BIOMASS RAW MATERIAL PARTICLE(6,3)|COOL BIOMASS RAW MATERIAL(6,3)|ENVIRONMENT TEMPERATURE(6,3)|EXTRACELLULAR ENZYME SECRETION(6,2)|HARDENING INHIBITION(6,2)|MICROBIAL DECOMPOSITION(6,2)|NUTRIENT UTILIZATION(6,2)|ACIDIFICATION INHIBITION ASSAY(6,1)|COMPOSTING HUMIFICATION(6,1)|FLORA DORMANCY(6,1)|NEUTRALIZATION TITRATIONCONCENTRATION(6,1)|GRAIN SIZE(5,22)|CARBON INCREMENT(5,3)|ORGANIC CARBON(5,3)|CARBON SINK FUNCTION(5,2)|FUNCTIONAL FLORA(5,2)|NUTRIENT REQUIREMENT(5,2)|REGULATION DIRECTION(5,2)|STRAW POWDER(5,2)|ACCELERATE MINERALIZATION(5,1)|AEROBIC FUNCTIONAL BACTERIUM(5,1)|BACILLUS METABOLITE(5,1)|BIOCHAR ADSORPTION CAPACITY(5,1)|BIOCHAR FERTILIZER(5,1)|BIOCHAR PORE(5,1)|BIOCHAR PROTECTION(5,1)|BIOCHAR WETTING(5,1)|CARBON SEQUESTRATION BIDIRECTIONAL OPTIMIZATION(5,1)|COVERING PRETREATED STRAW(5,1)|CULTIVATION DISTURBANCE(5,1)|DEEP SOIL ANAEROBIC ENVIRONMENT(5,1)|DEEP SOIL ANOXIC ENVIRONMENT(5,1)|EXTRACELLULAR POLYSACCHARIDE(5,1)|FUNGUS DREG(5,1)|HYDROLYZABLE ACIDTAKING(5,1)|HYPOXIA TOLERANT FUNCTIONAL BACTERIUM(5,1)|INCOMPLETE CARBONIZATION(5,1)|LAYERED FERTILIZATION(5,1)|MICROBIAL COLONIZATION(5,1)|MICROORGANISM ADHESION(5,1)|MICROORGANISM TOLERANCE(5,1)|MIXED BACTERIUM POLLUTION(5,1)|MOISTURE PERMEATION INTERACTION(5,1)|NPK FERTILIZER(5,1)|NUTRIENT SYNERGISTIC RELEASE(5,1)|PORE VENTILATION(5,1)|PYROLYSIS CARBONIZATION(5,1)|PYROLYSIS UNIFORMITY(5,1)|SMALL GRAIN ORGANIC FERTILIZER(5,1)|SOIL FERTILIZER RETAINING CAPACITY(5,1)|THERMOCHEMICAL DECOMPOSITION(5,1)|UNDISTURBED SOIL COLUMN(5,1)|DEEP LAYER(4,6)|VOLUME RATIO(4,4)|CELLULASE(4,3)|CONSTANT TEMPERATURE(4,3)|ALKALINE ENVIRONMENT(4,2)|BACILLUS AMYLOLIQUEFACIENS(4,2)|CARBON DECOMPOSITION(4,2)|CROP GROWTH(4,2)|LARGE GRAIN DIAMETER(4,2)|CRUSHING RICE STRAW(4,1)|DEEP NUTRIENT LOSS RISK(4,1)|DRY LAND SUBMERSION(4,1)|HARDENING RELIEF(4,1)|HOG MANURE(4,1)|HYPOXIA RESISTANT FUNCTIONAL BACTERIUM(4,1)|INSOLUBLE NUTRIENT(4,1)|MICROORGANISM LOADING(4,1)|NITROGEN COMETABOLISM(4,1)|QUICKLY RELEASING NUTRIENT(4,1)|RICE EARLY GROWTH(4,1)|SINGLE APPLICATION PROGRAM STRATEGY(4,1)|SOIL BORNE PATHOGENIC BACTERIUM(4,1)|VERIFYING EXPERIMENT(4,1)|WEED SEED(4,1)|SURFACE SOIL(3,12)|GRAIN SIZE BIOCHAR(3,7)|MASS RATIO(3,6)|LARGE PARTICLE SIZE BIOCHAR(3,3)|PART RATIO(3,3)|PYROLYSIS TIME(3,3)|SHORT SECTION(3,3)|DEEP SOIL AIR PERMEABILITY(3,2)|MICROPORE(3,2)|SLOW RELEASE BARRIER(3,2)|SUPERNATANT(3,2)|WATER CONDUCTION(3,2)|ADOPTING ORGANIC FERTILIZER(3,1)|AGGLOMERATE SEPARATION(3,1)|BALANCE NUTRIENT(3,1)|BIOCHAR PHYSICAL ADSORPTION CAPACITY(3,1)|BIOCHAR PYROLYSIS TEMPERATURE(3,1)|CLAY MINERAL(3,1)|COMPOSITE COLLOID(3,1)|DEEP SOIL CARBON MINERALIZATION(3,1)|GROUND MINERAL(3,1)|INERT NUTRIENT(3,1)|LAYER NUTRIENT COMPETITION(3,1)|NITROGEN COMPETITION(3,1)|NITROGEN MORPHOLOGY(3,1)|PHENOLIC HYDROXYL(3,1)|PORE ADSORPTION(3,1)|PROTECT MICROORGANISM(3,1)|PYROLYSIS BIOCHAR POROUS STRUCTURE(3,1)|SETTLING(3,1)|STRAW CELLULOSE(3,1)|VOLATILIZATION LOSS(3,1)|WET CARBON CAKING(3,1)|COOLING TIME(2,3)|ACIDIC ENVIRONMENT(2,1)|AMMONIA NITROGEN(2,1)|AMMONIA RELEASE(2,1)|APERTURE SIEVE(2,1)|ASH CONTENT(2,1)|BACTERIAL LIQUID VIABLE COUNT(2,1)|BASIC ASH(2,1)|DECARBOXYLATION(2,1)|DECOMPOSITION RESISTANCE(2,1)|DEEP CARBON STABILITY(2,1)|DEEP SOIL POROSITY(2,1)|DRY LAND MASS(2,1)|EXCHANGEABLE ACID(2,1)|EXTRACTION COLUMN(2,1)|HUMUS FORMATION(2,1)|IMPLEMENTATION SITE(2,1)|ISTHE DROP(2,1)|LOW CARBON(2,1)|METHANOGENESIS PATH(2,1)|METHANOL WATER EXTRACTING(2,1)|MICROBIAL LOAD(2,1)|MICROENVIRONMENT(2,1)|MICROORGANISM FUNCTIONAL ACTIVITY PERIOD(2,1)| (CN120548812)|1. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer is characterized by comprising the following steps of:| Step 1, crushing a biomass raw material, pyrolyzing the biomass raw material at 500-700 ℃ for 5-8 hours, and cooling the biomass raw material to obtain biochar; | step 2, preparing functional bacterial liquid containing actinomycetes and bacillus according to the part ratio of (1-3): 1, wherein the number of viable bacteria of the functional bacterial liquid ;|Step 3, immersing the biochar in the functional bacterial liquid for activation treatment, and controlling the volume ratio of the functional bacterial liquid to the biochar to be 1 (2-3) to obtain modified biochar;| Step 4, mixing the modified biochar with the decomposed straw, composting and fermenting, granulating and screening after the completion of the composting to obtain organic fertilizers with different particle sizes; | step 5, applying organic fertilizer with large grain size into deep soil, paving pretreated straw on the soil, covering the soil, and applying organic fertilizer with small grain size into surface soil; | in the step 3, the environment temperature of the activation treatment is controlled to be 25-30 ℃, the activation treatment is carried out for 18-24 hours at the constant temperature of 25-30 ℃, and the modified biochar is dehydrated until the water content is 5-10%. |2. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer according to claim 1, wherein,|In the step 1, the lignin content of the biomass raw material is more than or equal to 30%, the crushed biomass raw material is sieved by a 15-20 mesh sieve, and the particle size of the crushed biomass raw material particles is less than or equal to 5 mm.|3. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer according to claim 1, wherein,|In the step 1, the pyrolysis time is controlled to be 6-7 hours, and nitrogen is introduced to cool the biomass raw material after the pyrolysis is finished, and the cooling time is controlled to be less than 30 minutes.|4. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer according to claim 1, wherein,|In the step 4, the proportion of the modified biochar, the decomposed straw compost and the edible fungus residues is (5-6) and (3-4) is 1, the mixture is uniformly mixed until the uniformity is more than or equal to 95%, the water content of the materials is regulated to 50-60%, the composting fermentation lasts for 5-7 days, the temperature of the composting is controlled to be 55-65 ℃, and the composting is turned once every day.|5. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer according to claim 1, wherein,|In the step 5, the particle size of the large-particle-size organic fertilizer is 4 to 6 millimeters, and the particle size of the small-particle-size organic fertilizer is 2 to 4 millimeters;| applying organic fertilizer with large grain diameter to deep soil with 20-30 cm according to the dosage of 1200+ -50 kg per hectare; | Paving pretreated straws at the position of a soil layer of 10-20 cm according to the dosage of 2000+/-100 kg per hectare; | applying small-grain organic fertilizer into surface soil of 0-10 cm according to the dosage of 800+/-30 kg per hectare. |6. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer according to claim 1, wherein,|In the step 5, the pretreatment of the straw is that the complete straw is cut into short sections of 2-5 cm, and naturally dried in the sun until the water content is less than or equal to 30 percent.|7. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer according to claim 1, wherein,|In the step 4, the pretreatment of the decomposed straw comprises the steps of mixing the decomposed straw with a decomposing agent according to the mass ratio of (10-15) to 1, adjusting the carbon nitrogen ratio to (25-30) to 1, piling and fermenting for 2-3 days, wherein the decomposing agent comprises a composite microbial inoculum of bacillus subtilis and aspergillus oryzae, and the viable count of the bacillus subtilis and aspergillus oryzae。|8. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer according to claim 1, wherein,|In the composting fermentation process of the step 4, monitoring the pH value of the material, regulating the pH value to 6.5-7.5, adding straw powder to regulate ventilation when turning the pile every day, and stopping fermentation when the cellulose degradation rate in the material is more than or equal to 60%.|9. The rice field soil carburetion and dilatation method based on the biochar-based organic fertilizer according to claim 1, wherein,|In step 5, after fertilization, the pretreated straw layer with the thickness of 3-5 cm is covered on the surface soil, and the water content of the soil is kept between 60% and 70% by regular sprinkling irrigation for 15-20 days. (CN120548812)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of soil function improvement, in particular to a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer.|BACKGROUND ART|[0002] In recent years, with the deep research of the soil ecosystem and the increase of the sustainable development demand of agriculture, carburetion and capacity expansion become key paths for improving the soil quality. The biochar is rich in carbon elements, so that carbon increment can be realized after the biochar is applied to soil, the porous structure of the biochar can optimize the soil pore condition, and the capacity of the soil are expanded, so that the physical property, the chemical property and the biological function of the soil are systematically improved.|[0003] However, the traditional technology generally applies organic fertilizer or biochar to surface layer or shallow soil uniformly, microorganisms in deep soil are led by anaerobic bacteria due to lack of oxygen, the decomposition capacity of the deep soil is obviously limited, the mineralization rate of organic carbon loaded by large-particle-size biochar is extremely low, carbon and nitrogen nutrients are retained in the deep layer for a long time, dislocation is formed with the requirement of a rice root system distribution area (0-20 cm surface layer), and the nutrient leaching risk is caused.|[0004] To address this problem, existing methods attempt to adjust large particle size biochar fertilizers to small particle size. Although the small-particle-size biochar can improve the surface layer carbon fixation efficiency, after being applied to a deep layer, fine particles are easy to combine with clay minerals to form a compact aggregate structure, so that the soil porosity is greatly reduced, and moisture permeation and gas exchange are prevented. The deep soil anoxic environment further inhibits the metabolic activity of aerobic functional bacteria, simultaneously stimulates the methanogenesis path leading by anaerobic bacteria, and finally leads to negative linkage effects such as soil acidification, structural degradation and the like.|DISCLOSURE|Disclosure of Invention|[0005] In view of the technical problems that in the prior art, the traditional soil carburetion technology has low carbon holding efficiency, aggravated acidification and hardening and mismatch of carbon and nitrogen nutrient supply and demand of deep soil due to a single application strategy, and has negative influence.|[0006] The application provides a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer, which comprises the following steps:|[0007] Step 1, crushing a biomass raw material, pyrolyzing at 500-700 ℃ for 5-8 h, and cooling to obtain biochar; |[0008] step 2, preparing functional bacterial liquid containing actinomycetes and bacillus according to the part ratio of (1-3): 1, wherein the number of viable bacteria of the functional bacterial liquid is more than or equal to ;|[0009] Step 3, immersing the biochar in the functional bacterial liquid for activation treatment, and controlling the volume ratio of the functional bacterial liquid to the biochar to be 1 (2-3) to obtain modified biochar;|[0010] Step 4, mixing the modified biochar with the decomposed straw, composting and fermenting, granulating and screening after the completion of the composting to obtain organic fertilizers with different particle sizes; |[0011] And 5, applying the organic fertilizer with large grain size into deep soil, paving the pretreated straw on the soil, covering the soil, and applying the organic fertilizer with small grain size into surface soil. |[0012] Further, in the step 1, the lignin content of the biomass raw material is more than or equal to 30%, the biomass raw material is crushed and then screened by a 15-20 mesh screen, and the particle size of the crushed biomass raw material particles is less than or equal to 5 mm.|[0013] Further, in the step 1, the pyrolysis time is controlled to be 6-7 hours, and nitrogen is introduced to cool the biomass raw material after the pyrolysis is finished, and the cooling time is controlled to be less than 30 minutes.|[0014] Further, in the step 3, the environment temperature of the activation treatment is controlled to be 25-30 ℃, the activation treatment is carried out for 18-24 hours at the constant temperature of 25-30 ℃, and the modified biochar is dehydrated until the water content is 5-10%.|[0015] Further, in the step 4, the proportion of the modified biochar, the decomposed straw compost and the edible fungus residues is (5-6): (3-4): 1, the mixture is uniformly mixed until the uniformity is more than or equal to 95%, the water content of the materials is regulated to 50% -60%, the composting fermentation lasts for 5-7 days, the temperature of the composting is controlled to be 55-65 ℃, and the composting is turned once every day.|[0016] Further, in step 5, the particle size of the large-particle-size organic fertilizer is 4 to 6 mm, and the particle size of the small-particle-size organic fertilizer is 2 to 4 mm;|[0017] applying organic fertilizer with large grain diameter to deep soil with 20-30 cm according to the dosage of 1200 kg + -50 kg per hectare; |[0018] paving pretreated straws at the position of a soil layer of 10 to 20 cm according to the dosage of 2000 kg+/-100 kg per hectare; |[0019] applying the organic fertilizer with small grain size into the surface soil with the grain size of 0-10 cm according to the dosage of 800 kg + -30 kg per hectare. |[0020] Further, in the step 5, the step of straw pretreatment is to cut the whole straw into short sections of 2-5 cm, and naturally airing the whole straw in the sun until the water content is less than or equal to 30%.|[0021] Further, in the step 4, the pretreatment of the decomposed straw comprises the steps of mixing the decomposed straw with a decomposing agent according to the mass ratio of (10-15): 1, adjusting the carbon nitrogen ratio to be (25-30): 1, and carrying out stacking fermentation for 2-3 days for use, wherein the decomposing agent comprises a composite microbial inoculum of bacillus subtilis and aspergillus oryzae, and the viable count is more than or equal to。|[0022] Further, in the composting fermentation process of the step4, the pH value of the material is monitored and is regulated to 6.5-7.5, straw powder is added to regulate ventilation when the material is turned over every day, and the fermentation is stopped when the cellulose degradation rate in the material is more than or equal to 60%.|[0023] Further, in step 5, after fertilization, the surface soil is covered with a pretreated straw layer with a thickness of 3-5 cm, and the soil water content is kept at 60% -70% by regular sprinkling irrigation for 15-20 days.|[0024] The beneficial effects of the application are as follows:|[0025] The application relates to a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer, which comprises the steps of crushing biomass raw materials, pyrolyzing and cooling to obtain biochar, preparing functional bacteria liquid containing actinomycetes and bacillus, immersing the biochar in the functional bacteria liquid for activation treatment to obtain modified biochar, mixing the modified biochar with decomposed straws for composting fermentation, granulating and screening to obtain organic fertilizers with different particle sizes, applying the organic fertilizers with large particle sizes into deep soil, paving the pretreated straws on the soil, covering the soil with the organic fertilizers with small particle sizes, and mixing the organic fertilizers with surface soil. |[0026] The application solves the synergistic contradiction between deep soil carbon holding and nutrient utilization by applying the differentiation strategy of large-grain-size and small-grain-size biochar in a layered manner and combining the directional regulation and control of hypoxia-tolerant functional bacteria, the large-grain-size biochar forms a slow-release barrier in a deep layer to reduce carbon decomposition and nutrient loss, the porous structure of the large-grain-size biochar improves deep soil air permeability, promotes the metabolic activity of anaerobic flora, accelerates the carbon-nitrogen conversion efficiency, the small-grain-size biochar optimizes a surface layer soil pore network, enhances the interaction of moisture permeation and root system, and relieves the inhibition of hardening on microbial activity. The functional flora strengthens the decomposition of organic matters by secreting extracellular enzymes, and is accurately adapted to the nutrient requirements of the crop growth cycle. According to the application, the deep soil structure is repaired by the large-particle-size biochar and the carbon reservoir capacity is enlarged through a layered application strategy, and meanwhile, carbon and nitrogen co-metabolism driven by functional bacteria is utilized to improve carbon stability, so that the carbon holding efficiency is improved, the carbon increment and capacity expansion of soil are realized, the contradiction between carbon sequestration and structural degradation and nutrient imbalance in the traditional carbon increment and capacity expansion technology is solved, and the carbon sink function and agricultural productivity are promoted to be co-improved.|DRAWINGS DESCRIPTION|[0027] In order that the contents of the present invention may be more clearly understood, the present invention will be further described in detail with reference to the following detailed description of the present invention taken in conjunction with the accompanying drawings.|[0028] Fig. 1 is a process flow diagram of a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer.|INVENTION MODE|Detailed Description|[0029] The present invention will be further described in connection with the accompanying drawings and detailed description so that those skilled in the art may better understand and practice the invention, but are not limited thereto.|[0030] To this end, referring to fig. 1, the present application refers to a rice field soil carburetion and dilatation method based on biochar-based organic fertilizer, comprising:|[0031] and 1, crushing the biomass raw material, pyrolyzing at 500-700 ℃ for 5-8 hours, and cooling to obtain the biochar. |[0032] Under the condition of 500-700 ℃, pyrolysis can promote thermochemical decomposition of biomass raw materials, and complex organic matters such as lignin and the like are converted into stable aromatic carbon structures to form porous biochar with high specific surface area. Micropores and mesopores are generated by pyrolysis at high temperature to form a pore structure, so that the physical adsorption capacity of the biochar can be enhanced, and a microenvironment is provided for subsequent microbial colonization. The aromatic ring structure improves the carbon stability, can resist microbial decomposition, reduces deep soil carbon mineralization, and realizes long-acting carbon fixation. Part of nitrogen and phosphorus are converted into a slow-release state in the pyrolysis process, inert nutrients are reserved, and the risk of deep nutrient loss is reduced.|[0033] It should be noted that the pyrolysis temperature of biochar is controlled at 500-700 ℃, avoiding excessive decarboxylation to produce strongly basic ash due to excessive temperature (> 800 ℃). In addition, the high-temperature pyrolysis provides a carrier with high specific surface area for subsequent microorganism loading, the porous structure of the carrier can enhance microorganism adhesion efficiency, and the alkaline environment (pH 8-10) generated by high-temperature carbonization can partially inactivate pathogenic bacteria and reduce the mixed bacteria pollution in the composting fermentation stage.|[0034] In the technical scheme, in the step 1, the lignin content of the biomass raw material is more than or equal to 30%, the carbon stability of the high lignin raw material after pyrolysis is higher, and the decomposition resistance is stronger, wherein the biomass raw material can be straw or rice husk. And screening by using a 20-mesh screen after crushing, wherein the particle size of the crushed biomass raw material particles is less than or equal to 5 mm, so that the pyrolysis uniformity is improved, partial incomplete carbonization is avoided, and the contact area of the subsequent bacterial liquid during activation is improved.|[0035] In the step 1, the pyrolysis time is controlled to be 6-7 hours, and after the pyrolysis is finished, nitrogen is introduced or spraying is carried out to cool the biomass raw material, and the cooling time is controlled to be less than 30 minutes. The rapid cooling can reduce high-temperature oxidation, retain oxygen-containing functional groups such as carboxyl and phenolic hydroxyl on the surface, and enhance the adsorption capacity of the biochar on functional bacteria.|[0036] Step 2, preparing functional bacterial liquid containing actinomycetes and bacillus according to the part ratio of (1-3): 1, wherein the viable count of the bacterial liquid is more than or equal to;|[0037] Illustratively, in the present application, the actinomycetes may be selected from Streptomyces and the Bacillus may be selected from Bacillus amyloliquefaciens. Actinomycetes secrete cellulase and chitinase to decompose complex organic matters, promote the formation of humus, generate biosurfactant and improve the agglomeration of soil particles. The bacillus can antagonize soil-borne pathogenic bacteria, induce systemic resistance of plants, regulate and control nitrogen morphology through nitrification/denitrification, and reduce the risk of deep anaerobic methanogenesis.|[0038] In addition, the bacterial liquid is combined with the biochar in the step 3 to form a carbon-bacteria complex, and the pore structure of the biochar is utilized to protect microorganisms from being inhibited by the anaerobic environment of deep soil, so that the functional activity period of the microorganisms is prolonged.|[0039] And 3, immersing the biochar in functional bacterial liquid for activation treatment, and controlling the volume ratio of the bacterial liquid to the biochar to be 1 (2-3) to obtain the modified biochar.|[0040] In the technical scheme, in the step 3, the environment temperature of the activation treatment is controlled to be 25-30 ℃, the temperature is kept between 25-30 ℃ for 24 hours, and the modified biochar is dehydrated until the water content is between 5% and 10%.|[0041] The water content is controlled between 5% and 10%, so that the caking of wet carbon in compost can be avoided, the air permeability is influenced, and enough water is reserved to maintain the dormancy activity of flora.|[0042] At the constant temperature of 25-30 ℃, the volume ratio of the bacterial liquid to the biochar is 1 (2-3), so as to avoid the excessive bacterial liquid from causing excessive wetting of the biochar, influencing the ventilation of pores or causing insufficient load of bacterial groups. The bacterial liquid permeates into the pores of the biochar, and microorganisms colonize to form a biological membrane structure, so that the tolerance of the microorganisms to drought, hypoxia and other adverse conditions can be enhanced. Enzymes secreted by actinomycetes are combined with carboxyl and hydroxyl on the surface of biochar, so that the activation efficiency of phosphorus and potassium is improved, and bacillus metabolites can chelate insoluble nutrients in soil. The constant temperature treatment for 24 hours promotes the uniform evaporation of water, dehydrates and controls the humidity, avoids the agglomeration of biochar particles and maintains the connectivity of pores.|[0043] Step 4, mixing the modified biochar with the decomposed straw, composting and fermenting, granulating and screening after the completion of the composting to obtain organic fertilizers with different particle sizes;|[0044] In the technical scheme, in the step 4, the proportion of the modified biochar, the decomposed straw compost and the edible fungus residues is (5-6) in percentage by mass, 1 is mixed uniformly until the uniformity is more than or equal to 95%, the water content of the materials is regulated to 50% -60%, the microbial activity is limited by the water content being lower than 50%, the anaerobic fermentation is caused by the water content being higher than 60%, the composting fermentation lasts for 5-7 days, the composting temperature is controlled to be between 55-65 ℃, the degradation of cellulose by thermophilic bacteria is promoted, functional bacteria are inactivated by the excessive temperature of the composting body, and the composting heat dissipation is needed. |[0045] The modified biochar is mixed with decomposed straw and edible fungus residues according to the proportion of (5-6) to (3-4) to (1), and the synergistic release of nutrients is realized through high-temperature composting at 55-65 ℃. Straw cellulose is decomposed into humic acid under the action of microorganisms, and is combined with functional groups on the surface of biochar to generate a humification process, so that stable organic-inorganic composite colloid is formed, and the water and fertilizer retaining capacity of soil is improved. The fungus dreg provides a quick-acting nitrogen source, the straw provides a carbon skeleton, the biochar fixes ammonia nitrogen and balances nutrients, and the volatilization loss of nitrogen in the composting process can be reduced. The weed seeds and pathogenic bacteria are killed in the high-temperature stage (the period lasts for 3 days above 55 ℃), and ammonia release is reduced by combining the adsorption of biochar.|[0046] In the step 4, the pretreatment of the decomposed straw comprises the steps of mixing the decomposed straw with a decomposing agent according to the mass ratio of (10-15) 1, adjusting the carbon nitrogen ratio to be (25-30) 1, piling and fermenting for 2-3 days, wherein the decomposing agent comprises a composite microbial inoculum of bacillus subtilis and aspergillus oryzae, the mass ratio is 1:1, and the viable count is more than or equal to 1。|[0047] In the composting process, actinomycetes degrade lignin by secreting laccase, manganese peroxidase and the like to break the intractable structure of the straw, and bacillus hydrolyzes cellulose into glucose by utilizing a cellulase system. The bacillus provides carbon source for actinomycetes, biochar is used as a carrier, bacterial colony is fixed, pH is buffered, intermediate products are degraded through pore adsorption, and feedback inhibition is avoided.|[0048] Further, in the composting fermentation process of the step 4, the pH value of the material is monitored and is regulated to 6.5-7.5, straw powder is added to regulate ventilation when the material is turned over every day, and the fermentation is stopped when the cellulose degradation rate in the material is more than or equal to 60%. An acidic environment with a pH <6.5 will inhibit actinomycetes and a slightly alkaline environment with a pH >7.5 will reduce cellulase activity. The degradation rate of cellulose is controlled to be more than or equal to 60 percent, so that the straw is fully decomposed, and nitrogen competition after the straw is applied to the soil is avoided.|[0049] And 5, applying organic fertilizer with large grain size into deep soil, paving pretreated straw on the soil, covering the soil, adopting organic fertilizer with small grain size, and mixing the organic fertilizer with surface soil.|[0050] In the technical scheme, in the step 5, the particle size of the large-particle-size organic fertilizer is 4 to 6 millimeters, and the particle size of the small-particle-size organic fertilizer is 2 to 4 millimeters.|[0051] Applying large-grain organic fertilizer to deep soil of 20-30 cm according to the dosage of 1200 kg + -50 kg per hectare, and slowly decomposing the large grains in deep layer to form a long-term carbon warehouse to reduce CO 2 release. According to the dosage of 2000 kg+/-100 kg per hectare, paving pretreated straw at the position of soil layer of 10-20 cm, uniformly paving short-section straw, low water content and preventing the heat generation and root burning of fermentation, and according to the dosage of 800 kg+/-30 kg per hectare, applying small-grain-size organic fertilizer into surface soil of 0-10 cm, quickly releasing nutrients by small grains and promoting early growth of rice.|[0052] In the technical scheme, in the step 5, the step of pretreatment of the straw is that the complete straw is cut into short sections of 2-5 cm, and naturally dried in the sun until the water content is less than or equal to 30%.|[0053] In the application, large and small particle size organic fertilizers are differentially applied, straw pretreatment is combined, large particle size organic fertilizers (4-6 mm) are deeply applied (20-30 cm), large particle biochar can increase deep soil porosity, relieve anaerobic environment, inhibit methanogen activity, slow release nitrogen, phosphorus and potassium loaded by biochar diffuse to lateral areas of root systems along with moisture, slow release nutrients and reduce surface layer nutrient competition. The surface layer (0-10 cm) is applied with small-particle-size organic fertilizer (2-4 mm), small-particle biochar fills the pores of the surface layer, micropores are reserved for carbon, water evaporation and nutrient leaching are reduced, meanwhile, sunlight is reflected to reduce soil surface temperature fluctuation, and the organic fertilizer is mixed with pretreated straws (2-5 cm for a short period) to promote interaction of shallow root systems of rice and microorganisms. The straw pretreatment adopts a mode of cutting short sections and naturally airing to reduce the water content, accelerates the field decomposition and avoids the excessive compaction of surface soil.|[0054] The pyrolysis carbonization realizes physical stability, the microbial load carries out biological activation, and the composting humification reaches chemical balance. The deep large-grain-size carbon improves ventilation, the surface small-grain-size carbon inhibits hardening, and the pretreatment of the straw bridges organic matter gradient.|[0055] In step 5, after fertilization, the pretreated straw layer with the thickness of 3-5 cm is covered on the surface soil, and the water content of the soil is kept between 60% and 70% by regular sprinkling irrigation for 15-20 days.|[0056] The straw is covered by 3-5 cm parts, the covering layer can reduce water evaporation, and the sprinkling irrigation maintains the microbial activity so as to accelerate the mineralization of the organic fertilizer.|[0057] The application solves the synergistic contradiction between deep soil carbon holding and nutrient utilization by layering application of a differentiation strategy of large-grain-size and small-grain-size biochar and directional regulation of hypoxia-resistant functional bacteria, wherein the large-grain-size biochar forms a slow-release barrier in deep layers, reduces carbon decomposition and nutrient loss, has a porous structure for improving deep soil air permeability, promotes the metabolic activity of anaerobic flora, accelerates the carbon-nitrogen conversion efficiency, and the small-grain-size biochar optimizes a surface soil pore network, enhances moisture permeation and root system interaction, and relieves inhibition of hardening on microbial activity. The functional flora strengthens organic matter decomposition by secreting extracellular enzymes, is accurately adapted to nutrient requirements of crop growth periods, synchronously improves deep carbon stability and surface soil health, and finally realizes bidirectional optimization of carbon sequestration efficiency and agricultural productivity.|[0058] For a better understanding of the technical solution, exemplary embodiments of the present invention will be described in more detail below with reference to the accompanying drawings.|[0059] The implementation site and materials;|[0060] The site is a black soil area of Heilongjiang province, belongs to typical black soil, has the conventional pH of 5.5-6.0 and has the organic matter content of 3-4 percent. |[0061] The material comprises rice straw and pig manure compost thoroughly decomposed straw in biomass raw materials, and Streptomyces griseus and bacillus amyloliquefaciens in functional bacterial liquid with the fraction ratio of 1:1.|[0062] Each group is provided with 3 groups of parallel experiments, the total period of the experiments is 12 months, the straws are crushed, the biochar is prepared and decomposed, the straws are pretreated, the layers are fertilized, the soil is covered, the rice (variety: longjing tea 20) is planted, and the data acquisition is carried out once every 3 months.|[0063] Experiment design;|[0064] The embodiment group comprises that large-grain-size organic fertilizer (4-6 mm) Shi Shenceng (20-30 cm) +small-grain-size organic fertilizer (2-4 mm) Shi Biaoceng (0-10 cm) +straw cover (3-5 cm) +functional bacterial liquid is activated. |[0065] Control group 1, traditional fertilizer (NPK), traditional single fertilization.|[0066] Control group 2, layered fertilization (large particle size + small particle size organic fertilizer) +surface soil covering, but no functional bacteria liquid is added.|[0067] Embodiments are described herein;|[0068] and (3) preparing biochar, crushing rice straw to be less than or equal to 5 mm, pyrolyzing at 500 ℃ for 6 hours, protecting with nitrogen, cooling to room temperature, crushing and sieving with a 20-mesh sieve. |[0069] Pretreatment of decomposed straw, wherein the decomposed straw and a decomposing agent contain bacillus subtilis and aspergillus oryzae in a mass ratio of 1:1, and viable count is carried outMixing at 10:1, adjusting C/N=25:1, and fermenting for 3 days. Modified biochar (5-6 mm), decomposed straw compost and edible fungus residues are mixed according to a ratio of 6:3:1, the water content is adjusted to be 55%, and the composting fermentation is carried out for 7 days, and the composting is carried out every day.|[0070] Applying fertilizer in the field, wherein the embodiment group comprises deep layer (20-30 cm) Shi Da particle size organic fertilizer (1200 kg/ha), surface layer (0-10 cm) Shi Xiao particle size organic fertilizer (800 kg/ha), and covering pretreated straw (3-5 cm) after earthing;|[0071] the control group 1 is that NPK fertilizer (300 kg/ha) is evenly applied to the surface layer; |[0072] the control group 2 has the same fertilizing amount as the example group, but no functional bacterial liquid is added. |[0073] And (3) measuring carburetion efficiency, namely measuring the Total Organic Carbon (TOC) content of a soil sample by adopting a potassium dichromate oxidation-external heating method, air-drying, grinding and sieving (2 mm) the soil sample, oxidizing the organic carbon by using concentrated sulfuric acid and a potassium dichromate solution, and measuring the TOC content by a titration method. The water extract was filtered through a 0.45 μm filter, and the content of dissolved carbon (DOC) in the filtrate was measured by a total organic carbon analyzer, and the data are shown in table 1.|[0074] ;|[0075] Referring to Table1, the TOC of the example group was 25.3g/kg, the control group 1 was 18.7 g/kg, and the improvement was 35.3% (p < 0.05). The porous structure of the pyrolysis biochar adsorbs organic molecules, so that microbial decomposition is reduced, scanning electron microscopy verifies that pores are filled, the large-particle-size organic fertilizer is applied to deep soil, cultivation disturbance is reduced, and physical protection combination of the biochar and soil minerals is promoted. The TOC of the example group was significantly higher than that of control group 1, and the organic carbon storage in the soil was increased due to reduced decomposition of the organic carbon by adsorption of the biochar.|[0076] The DOC of the example group is 0.38 g/kg, the DOC of the control group 2 is 0.29 g/kg, and the improvement is 31.0%. Actinomycetes secrete Extracellular Polysaccharide (EPS), indicating that functional bacteria promote short-term retention of carbon.|[0077] An acidification inhibition assay; the pH value is measured by adopting a potentiometric method, a soil sample is naturally air-dried, filtered through a 2mm sieve, mixed with deionized water according to a mass ratio of 1:2.5, stirred for 30 minutes, and stood for 30 minutes, and the pH value of the suspension is measured by using a calibrated pH meter.|[0078] Determination of exchangeable acids by potassium chloride exchange methodAnd a hydrolyzable acidTaking air-dried soil sample 2.5 g with 2mm sieve, adding 1mol/LKCl solution 50 mL, oscillating for 2 hr, centrifuging to separate supernatant, and measuring exchange property by neutralization titrationConcentration (in cmol/kg);|[0079] Oxalic acid concentration was determined by High Performance Liquid Chromatography (HPLC). Subjecting the soil sample to methanol-water Extracting, centrifuging to obtain supernatant, purifying with C18 solid phase extraction column, concentrating, dissolving in mobile phase (0.1% formic acid water solution: acetonitrile=90:10), and quantifying oxalic acid concentration by HPLC (ultraviolet detector, lambda=210 nm), wherein the data are shown in Table 2.|[0080] ;|[0081] Referring to Table 2, the pH of the example group was 6.8, the pH of the control group 1 was 5.2, the elevation was 30.8% (p < 0.05), and the ash content generated by the thermal pyrolysis of biochar was rich、Neutralization of soil by ion exchange. Example group exchangeable acid 70.5% of control group 1, indicating that biochar was effective in reducing aluminum ionsAnd (5) dissolving out. The oxalic acid concentration of the example group was 12.3 mg/kg, the control group 2 was 22.1 mg/kg, and the reduction was 65.5% because the microorganism preferentially utilized the organic acid as the carbon source.|[0082] Anti-hardening experiment verification;|[0083] the hardening relief index measuring method comprises collecting original soil sample of 0-20 cm soil layers, and measuring volume The aluminum box is cut in layers to ensure the structural integrity of the soil, the fresh soil mass is weighed, recorded and then put into an oven (105 ℃) to be baked to constant weight for 48 hours, and the volume weight soil volume weight = dry soil mass (g)/annular cutter volume is calculated。|[0084] Taking an air-dried soil sample 20 g passing through a 2mm sieve, placing the air-dried soil sample into a settling cylinder, adding a 0.25 mm aperture sieve, injecting distilled water into the submerged soil, standing for 10 minutes, simulating the field moisture condition, slowly shaking the sieve, separating agglomerates, collecting fine particles passing through the sieve aperture, drying and weighing, and calculating the mass (g) of the agglomerates of more than 0.25 mm/the mass (g) of the total soil sample of more than 0.25 mm by 100 percent.|[0085] Placing undisturbed soil column with height of 10 cm and diameter of 10 cm in a permeameter, injecting distilled water into upper ring, keeping saturated state, collecting percolating water into lower ring, recording stable percolating time (about 30 min), and calculating water conductivity: Wherein Q is flow, L is soil column height, A is cross-sectional area, and h is head difference. The data are shown in Table 3. |[0086] ;|[0087] Referring to Table 3, the example set has a volume weight ofControl group 1 isThe drop is 20.7% (p < 0.05), and the granular structure is formed because the biochar fills the pores. The proportion of agglomerates in the example group greater than 0.25 mm is 50%, the proportion in the control group 2 is 42%, and the improvement is 19.0%. The water conductivity of the example group is 8.2 cm/h, the water conductivity of the control group 1 is 3.5 cm/h, and the improvement is 134%. The volume weight of the example group is reduced by 20.7% compared with that of the control group 1. Indicating that the decrease in permeability due to hardening is improved.|[0088] It should be understood that the foregoing is by way of example only and is not intended to limit the embodiments. Other variations and modifications of the present invention will be apparent to those of ordinary skill in the art in light of the foregoing description. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present invention.|[0089] In the description of the present invention, it should be understood that the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.|[0090] In the description of this specification, the terms "one," "some," "examples," "specific examples," or "some examples," etc., refer to a particular feature, structure, material, or characteristic described in connection with the or an example as being included in at least one or an example of the invention. In this specification, schematic representations of the above terms are not necessarily for the same example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more or examples. Furthermore, the different examples described in this specification and the features of the different examples may be combined and combined by those skilled in the art without contradiction.|[0091] It will be appreciated that the foregoing is illustrative and is not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made therein by those skilled in the art within the scope of the invention. (CN120548812)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of soil function improvement, in particular to a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer.|BACKGROUND ART|[0002] In recent years, with the deep research of the soil ecosystem and the increase of the sustainable development demand of agriculture, carburetion and capacity expansion become key paths for improving the soil quality. The biochar is rich in carbon elements, so that carbon increment can be realized after the biochar is applied to soil, the porous structure of the biochar can optimize the soil pore condition, and the capacity of the soil are expanded, so that the physical property, the chemical property and the biological function of the soil are systematically improved.|[0003] However, the traditional technology generally applies organic fertilizer or biochar to surface layer or shallow soil uniformly, microorganisms in deep soil are led by anaerobic bacteria due to lack of oxygen, the decomposition capacity of the deep soil is obviously limited, the mineralization rate of organic carbon loaded by large-particle-size biochar is extremely low, carbon and nitrogen nutrients are retained in the deep layer for a long time, dislocation is formed with the requirement of a rice root system distribution area (0-20 cm surface layer), and the nutrient leaching risk is caused.|[0004] To address this problem, existing methods attempt to adjust large particle size biochar fertilizers to small particle size. Although the small-particle-size biochar can improve the surface layer carbon fixation efficiency, after being applied to a deep layer, fine particles are easy to combine with clay minerals to form a compact aggregate structure, so that the soil porosity is greatly reduced, and moisture permeation and gas exchange are prevented. The deep soil anoxic environment further inhibits the metabolic activity of aerobic functional bacteria, simultaneously stimulates the methanogenesis path leading by anaerobic bacteria, and finally leads to negative linkage effects such as soil acidification, structural degradation and the like.|DISCLOSURE|Disclosure of Invention|[0005] In view of the technical problems that in the prior art, the traditional soil carburetion technology has low carbon holding efficiency, aggravated acidification and hardening and mismatch of carbon and nitrogen nutrient supply and demand of deep soil due to a single application strategy, and has negative influence.|[0006] The application provides a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer, which comprises the following steps:|[0007] Step 1, crushing a biomass raw material, pyrolyzing at 500-700 ℃ for 5-8 h, and cooling to obtain biochar; |[0008] step 2, preparing functional bacterial liquid containing actinomycetes and bacillus according to the part ratio of (1-3): 1, wherein the number of viable bacteria of the functional bacterial liquid is more than or equal to ;|[0009] Step 3, immersing the biochar in the functional bacterial liquid for activation treatment, and controlling the volume ratio of the functional bacterial liquid to the biochar to be 1 (2-3) to obtain modified biochar;|[0010] Step 4, mixing the modified biochar with the decomposed straw, composting and fermenting, granulating and screening after the completion of the composting to obtain organic fertilizers with different particle sizes; |[0011] And 5, applying the organic fertilizer with large grain size into deep soil, paving the pretreated straw on the soil, covering the soil, and applying the organic fertilizer with small grain size into surface soil. |[0012] Further, in the step 1, the lignin content of the biomass raw material is more than or equal to 30%, the biomass raw material is crushed and then screened by a 15-20 mesh screen, and the particle size of the crushed biomass raw material particles is less than or equal to 5 mm.|[0013] Further, in the step 1, the pyrolysis time is controlled to be 6-7 hours, and nitrogen is introduced to cool the biomass raw material after the pyrolysis is finished, and the cooling time is controlled to be less than 30 minutes.|[0014] Further, in the step 3, the environment temperature of the activation treatment is controlled to be 25-30 ℃, the activation treatment is carried out for 18-24 hours at the constant temperature of 25-30 ℃, and the modified biochar is dehydrated until the water content is 5-10%.|[0015] Further, in the step 4, the proportion of the modified biochar, the decomposed straw compost and the edible fungus residues is (5-6): (3-4): 1, the mixture is uniformly mixed until the uniformity is more than or equal to 95%, the water content of the materials is regulated to 50% -60%, the composting fermentation lasts for 5-7 days, the temperature of the composting is controlled to be 55-65 ℃, and the composting is turned once every day.|[0016] Further, in step 5, the particle size of the large-particle-size organic fertilizer is 4 to 6 mm, and the particle size of the small-particle-size organic fertilizer is 2 to 4 mm;|[0017] applying organic fertilizer with large grain diameter to deep soil with 20-30 cm according to the dosage of 1200 kg + -50 kg per hectare; |[0018] paving pretreated straws at the position of a soil layer of 10 to 20 cm according to the dosage of 2000 kg+/-100 kg per hectare; |[0019] applying the organic fertilizer with small grain size into the surface soil with the grain size of 0-10 cm according to the dosage of 800 kg + -30 kg per hectare. |[0020] Further, in the step 5, the step of straw pretreatment is to cut the whole straw into short sections of 2-5 cm, and naturally airing the whole straw in the sun until the water content is less than or equal to 30%.|[0021] Further, in the step 4, the pretreatment of the decomposed straw comprises the steps of mixing the decomposed straw with a decomposing agent according to the mass ratio of (10-15): 1, adjusting the carbon nitrogen ratio to be (25-30): 1, and carrying out stacking fermentation for 2-3 days for use, wherein the decomposing agent comprises a composite microbial inoculum of bacillus subtilis and aspergillus oryzae, and the viable count is more than or equal to。|[0022] Further, in the composting fermentation process of the step4, the pH value of the material is monitored and is regulated to 6.5-7.5, straw powder is added to regulate ventilation when the material is turned over every day, and the fermentation is stopped when the cellulose degradation rate in the material is more than or equal to 60%.|[0023] Further, in step 5, after fertilization, the surface soil is covered with a pretreated straw layer with a thickness of 3-5 cm, and the soil water content is kept at 60% -70% by regular sprinkling irrigation for 15-20 days.|[0024] The beneficial effects of the application are as follows:|[0025] The application relates to a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer, which comprises the steps of crushing biomass raw materials, pyrolyzing and cooling to obtain biochar, preparing functional bacteria liquid containing actinomycetes and bacillus, immersing the biochar in the functional bacteria liquid for activation treatment to obtain modified biochar, mixing the modified biochar with decomposed straws for composting fermentation, granulating and screening to obtain organic fertilizers with different particle sizes, applying the organic fertilizers with large particle sizes into deep soil, paving the pretreated straws on the soil, covering the soil with the organic fertilizers with small particle sizes, and mixing the organic fertilizers with surface soil. |[0026] The application solves the synergistic contradiction between deep soil carbon holding and nutrient utilization by applying the differentiation strategy of large-grain-size and small-grain-size biochar in a layered manner and combining the directional regulation and control of hypoxia-tolerant functional bacteria, the large-grain-size biochar forms a slow-release barrier in a deep layer to reduce carbon decomposition and nutrient loss, the porous structure of the large-grain-size biochar improves deep soil air permeability, promotes the metabolic activity of anaerobic flora, accelerates the carbon-nitrogen conversion efficiency, the small-grain-size biochar optimizes a surface layer soil pore network, enhances the interaction of moisture permeation and root system, and relieves the inhibition of hardening on microbial activity. The functional flora strengthens the decomposition of organic matters by secreting extracellular enzymes, and is accurately adapted to the nutrient requirements of the crop growth cycle. According to the application, the deep soil structure is repaired by the large-particle-size biochar and the carbon reservoir capacity is enlarged through a layered application strategy, and meanwhile, carbon and nitrogen co-metabolism driven by functional bacteria is utilized to improve carbon stability, so that the carbon holding efficiency is improved, the carbon increment and capacity expansion of soil are realized, the contradiction between carbon sequestration and structural degradation and nutrient imbalance in the traditional carbon increment and capacity expansion technology is solved, and the carbon sink function and agricultural productivity are promoted to be co-improved.|DRAWINGS DESCRIPTION|[0027] In order that the contents of the present invention may be more clearly understood, the present invention will be further described in detail with reference to the following detailed description of the present invention taken in conjunction with the accompanying drawings.|[0028] Fig. 1 is a process flow diagram of a rice field soil carburetion and dilatation method based on a biochar-based organic fertilizer.|INVENTION MODE|Detailed Description|[0029] The present invention will be further described in connection with the accompanying drawings and detailed description so that those skilled in the art may better understand and practice the invention, but are not limited thereto.|[0030] To this end, referring to fig. 1, the present application refers to a rice field soil carburetion and dilatation method based on biochar-based organic fertilizer, comprising:|[0031] and 1, crushing the biomass raw material, pyrolyzing at 500-700 ℃ for 5-8 hours, and cooling to obtain the biochar. |[0032] Under the condition of 500-700 ℃, pyrolysis can promote thermochemical decomposition of biomass raw materials, and complex organic matters such as lignin and the like are converted into stable aromatic carbon structures to form porous biochar with high specific surface area. Micropores and mesopores are generated by pyrolysis at high temperature to form a pore structure, so that the physical adsorption capacity of the biochar can be enhanced, and a microenvironment is provided for subsequent microbial colonization. The aromatic ring structure improves the carbon stability, can resist microbial decomposition, reduces deep soil carbon mineralization, and realizes long-acting carbon fixation. Part of nitrogen and phosphorus are converted into a slow-release state in the pyrolysis process, inert nutrients are reserved, and the risk of deep nutrient loss is reduced.|[0033] It should be noted that the pyrolysis temperature of biochar is controlled at 500-700 ℃, avoiding excessive decarboxylation to produce strongly basic ash due to excessive temperature (> 800 ℃). In addition, the high-temperature pyrolysis provides a carrier with high specific surface area for subsequent microorganism loading, the porous structure of the carrier can enhance microorganism adhesion efficiency, and the alkaline environment (pH 8-10) generated by high-temperature carbonization can partially inactivate pathogenic bacteria and reduce the mixed bacteria pollution in the composting fermentation stage.|[0034] In the technical scheme, in the step 1, the lignin content of the biomass raw material is more than or equal to 30%, the carbon stability of the high lignin raw material after pyrolysis is higher, and the decomposition resistance is stronger, wherein the biomass raw material can be straw or rice husk. And screening by using a 20-mesh screen after crushing, wherein the particle size of the crushed biomass raw material particles is less than or equal to 5 mm, so that the pyrolysis uniformity is improved, partial incomplete carbonization is avoided, and the contact area of the subsequent bacterial liquid during activation is improved.|[0035] In the step 1, the pyrolysis time is controlled to be 6-7 hours, and after the pyrolysis is finished, nitrogen is introduced or spraying is carried out to cool the biomass raw material, and the cooling time is controlled to be less than 30 minutes. The rapid cooling can reduce high-temperature oxidation, retain oxygen-containing functional groups such as carboxyl and phenolic hydroxyl on the surface, and enhance the adsorption capacity of the biochar on functional bacteria.|[0036] Step 2, preparing functional bacterial liquid containing actinomycetes and bacillus according to the part ratio of (1-3): 1, wherein the viable count of the bacterial liquid is more than or equal to;|[0037] Illustratively, in the present application, the actinomycetes may be selected from Streptomyces and the Bacillus may be selected from Bacillus amyloliquefaciens. Actinomycetes secrete cellulase and chitinase to decompose complex organic matters, promote the formation of humus, generate biosurfactant and improve the agglomeration of soil particles. The bacillus can antagonize soil-borne pathogenic bacteria, induce systemic resistance of plants, regulate and control nitrogen morphology through nitrification/denitrification, and reduce the risk of deep anaerobic methanogenesis.|[0038] In addition, the bacterial liquid is combined with the biochar in the step 3 to form a carbon-bacteria complex, and the pore structure of the biochar is utilized to protect microorganisms from being inhibited by the anaerobic environment of deep soil, so that the functional activity period of the microorganisms is prolonged.|[0039] And 3, immersing the biochar in functional bacterial liquid for activation treatment, and controlling the volume ratio of the bacterial liquid to the biochar to be 1 (2-3) to obtain the modified biochar.|[0040] In the technical scheme, in the step 3, the environment temperature of the activation treatment is controlled to be 25-30 ℃, the temperature is kept between 25-30 ℃ for 24 hours, and the modified biochar is dehydrated until the water content is between 5% and 10%.|[0041] The water content is controlled between 5% and 10%, so that the caking of wet carbon in compost can be avoided, the air permeability is influenced, and enough water is reserved to maintain the dormancy activity of flora.|[0042] At the constant temperature of 25-30 ℃, the volume ratio of the bacterial liquid to the biochar is 1 (2-3), so as to avoid the excessive bacterial liquid from causing excessive wetting of the biochar, influencing the ventilation of pores or causing insufficient load of bacterial groups. The bacterial liquid permeates into the pores of the biochar, and microorganisms colonize to form a biological membrane structure, so that the tolerance of the microorganisms to drought, hypoxia and other adverse conditions can be enhanced. Enzymes secreted by actinomycetes are combined with carboxyl and hydroxyl on the surface of biochar, so that the activation efficiency of phosphorus and potassium is improved, and bacillus metabolites can chelate insoluble nutrients in soil. The constant temperature treatment for 24 hours promotes the uniform evaporation of water, dehydrates and controls the humidity, avoids the agglomeration of biochar particles and maintains the connectivity of pores.|[0043] Step 4, mixing the modified biochar with the decomposed straw, composting and fermenting, granulating and screening after the completion of the composting to obtain organic fertilizers with different particle sizes;|[0044] In the technical scheme, in the step 4, the proportion of the modified biochar, the decomposed straw compost and the edible fungus residues is (5-6) in percentage by mass, 1 is mixed uniformly until the uniformity is more than or equal to 95%, the water content of the materials is regulated to 50% -60%, the microbial activity is limited by the water content being lower than 50%, the anaerobic fermentation is caused by the water content being higher than 60%, the composting fermentation lasts for 5-7 days, the composting temperature is controlled to be between 55-65 ℃, the degradation of cellulose by thermophilic bacteria is promoted, functional bacteria are inactivated by the excessive temperature of the composting body, and the composting heat dissipation is needed. |[0045] The modified biochar is mixed with decomposed straw and edible fungus residues according to the proportion of (5-6) to (3-4) to (1), and the synergistic release of nutrients is realized through high-temperature composting at 55-65 ℃. Straw cellulose is decomposed into humic acid under the action of microorganisms, and is combined with functional groups on the surface of biochar to generate a humification process, so that stable organic-inorganic composite colloid is formed, and the water and fertilizer retaining capacity of soil is improved. The fungus dreg provides a quick-acting nitrogen source, the straw provides a carbon skeleton, the biochar fixes ammonia nitrogen and balances nutrients, and the volatilization loss of nitrogen in the composting process can be reduced. The weed seeds and pathogenic bacteria are killed in the high-temperature stage (the period lasts for 3 days above 55 ℃), and ammonia release is reduced by combining the adsorption of biochar.|[0046] In the step 4, the pretreatment of the decomposed straw comprises the steps of mixing the decomposed straw with a decomposing agent according to the mass ratio of (10-15) 1, adjusting the carbon nitrogen ratio to be (25-30) 1, piling and fermenting for 2-3 days, wherein the decomposing agent comprises a composite microbial inoculum of bacillus subtilis and aspergillus oryzae, the mass ratio is 1:1, and the viable count is more than or equal to 1。|[0047] In the composting process, actinomycetes degrade lignin by secreting laccase, manganese peroxidase and the like to break the intractable structure of the straw, and bacillus hydrolyzes cellulose into glucose by utilizing a cellulase system. The bacillus provides carbon source for actinomycetes, biochar is used as a carrier, bacterial colony is fixed, pH is buffered, intermediate products are degraded through pore adsorption, and feedback inhibition is avoided.|[0048] Further, in the composting fermentation process of the step 4, the pH value of the material is monitored and is regulated to 6.5-7.5, straw powder is added to regulate ventilation when the material is turned over every day, and the fermentation is stopped when the cellulose degradation rate in the material is more than or equal to 60%. An acidic environment with a pH <6.5 will inhibit actinomycetes and a slightly alkaline environment with a pH >7.5 will reduce cellulase activity. The degradation rate of cellulose is controlled to be more than or equal to 60 percent, so that the straw is fully decomposed, and nitrogen competition after the straw is applied to the soil is avoided.|[0049] And 5, applying organic fertilizer with large grain size into deep soil, paving pretreated straw on the soil, covering the soil, adopting organic fertilizer with small grain size, and mixing the organic fertilizer with surface soil.|[0050] In the technical scheme, in the step 5, the particle size of the large-particle-size organic fertilizer is 4 to 6 millimeters, and the particle size of the small-particle-size organic fertilizer is 2 to 4 millimeters.|[0051] Applying large-grain organic fertilizer to deep soil of 20-30 cm according to the dosage of 1200 kg + -50 kg per hectare, and slowly decomposing the large grains in deep layer to form a long-term carbon warehouse to reduce CO 2 release. According to the dosage of 2000 kg+/-100 kg per hectare, paving pretreated straw at the position of soil layer of 10-20 cm, uniformly paving short-section straw, low water content and preventing the heat generation and root burning of fermentation, and according to the dosage of 800 kg+/-30 kg per hectare, applying small-grain-size organic fertilizer into surface soil of 0-10 cm, quickly releasing nutrients by small grains and promoting early growth of rice.|[0052] In the technical scheme, in the step 5, the step of pretreatment of the straw is that the complete straw is cut into short sections of 2-5 cm, and naturally dried in the sun until the water content is less than or equal to 30%.|[0053] In the application, large and small particle size organic fertilizers are differentially applied, straw pretreatment is combined, large particle size organic fertilizers (4-6 mm) are deeply applied (20-30 cm), large particle biochar can increase deep soil porosity, relieve anaerobic environment, inhibit methanogen activity, slow release nitrogen, phosphorus and potassium loaded by biochar diffuse to lateral areas of root systems along with moisture, slow release nutrients and reduce surface layer nutrient competition. The surface layer (0-10 cm) is applied with small-particle-size organic fertilizer (2-4 mm), small-particle biochar fills the pores of the surface layer, micropores are reserved for carbon, water evaporation and nutrient leaching are reduced, meanwhile, sunlight is reflected to reduce soil surface temperature fluctuation, and the organic fertilizer is mixed with pretreated straws (2-5 cm for a short period) to promote interaction of shallow root systems of rice and microorganisms. The straw pretreatment adopts a mode of cutting short sections and naturally airing to reduce the water content, accelerates the field decomposition and avoids the excessive compaction of surface soil.|[0054] The pyrolysis carbonization realizes physical stability, the microbial load carries out biological activation, and the composting humification reaches chemical balance. The deep large-grain-size carbon improves ventilation, the surface small-grain-size carbon inhibits hardening, and the pretreatment of the straw bridges organic matter gradient.|[0055] In step 5, after fertilization, the pretreated straw layer with the thickness of 3-5 cm is covered on the surface soil, and the water content of the soil is kept between 60% and 70% by regular sprinkling irrigation for 15-20 days.|[0056] The straw is covered by 3-5 cm parts, the covering layer can reduce water evaporation, and the sprinkling irrigation maintains the microbial activity so as to accelerate the mineralization of the organic fertilizer.|[0057] The application solves the synergistic contradiction between deep soil carbon holding and nutrient utilization by layering application of a differentiation strategy of large-grain-size and small-grain-size biochar and directional regulation of hypoxia-resistant functional bacteria, wherein the large-grain-size biochar forms a slow-release barrier in deep layers, reduces carbon decomposition and nutrient loss, has a porous structure for improving deep soil air permeability, promotes the metabolic activity of anaerobic flora, accelerates the carbon-nitrogen conversion efficiency, and the small-grain-size biochar optimizes a surface soil pore network, enhances moisture permeation and root system interaction, and relieves inhibition of hardening on microbial activity. The functional flora strengthens organic matter decomposition by secreting extracellular enzymes, is accurately adapted to nutrient requirements of crop growth periods, synchronously improves deep carbon stability and surface soil health, and finally realizes bidirectional optimization of carbon sequestration efficiency and agricultural productivity.|[0058] For a better understanding of the technical solution, exemplary embodiments of the present invention will be described in more detail below with reference to the accompanying drawings.|[0059] The implementation site and materials;|[0060] The site is a black soil area of Heilongjiang province, belongs to typical black soil, has the conventional pH of 5.5-6.0 and has the organic matter content of 3-4 percent. |[0061] The material comprises rice straw and pig manure compost thoroughly decomposed straw in biomass raw materials, and Streptomyces griseus and bacillus amyloliquefaciens in functional bacterial liquid with the fraction ratio of 1:1.|[0062] Each group is provided with 3 groups of parallel experiments, the total period of the experiments is 12 months, the straws are crushed, the biochar is prepared and decomposed, the straws are pretreated, the layers are fertilized, the soil is covered, the rice (variety: longjing tea 20) is planted, and the data acquisition is carried out once every 3 months.|[0063] Experiment design;|[0064] The embodiment group comprises that large-grain-size organic fertilizer (4-6 mm) Shi Shenceng (20-30 cm) +small-grain-size organic fertilizer (2-4 mm) Shi Biaoceng (0-10 cm) +straw cover (3-5 cm) +functional bacterial liquid is activated. |[0065] Control group 1, traditional fertilizer (NPK), traditional single fertilization.|[0066] Control group 2, layered fertilization (large particle size + small particle size organic fertilizer) +surface soil covering, but no functional bacteria liquid is added.|[0067] Embodiments are described herein;|[0068] and (3) preparing biochar, crushing rice straw to be less than or equal to 5 mm, pyrolyzing at 500 ℃ for 6 hours, protecting with nitrogen, cooling to room temperature, crushing and sieving with a 20-mesh sieve. |[0069] Pretreatment of decomposed straw, wherein the decomposed straw and a decomposing agent contain bacillus subtilis and aspergillus oryzae in a mass ratio of 1:1, and viable count is carried outMixing at 10:1, adjusting C/N=25:1, and fermenting for 3 days. Modified biochar (5-6 mm), decomposed straw compost and edible fungus residues are mixed according to a ratio of 6:3:1, the water content is adjusted to be 55%, and the composting fermentation is carried out for 7 days, and the composting is carried out every day.|[0070] Applying fertilizer in the field, wherein the embodiment group comprises deep layer (20-30 cm) Shi Da particle size organic fertilizer (1200 kg/ha), surface layer (0-10 cm) Shi Xiao particle size organic fertilizer (800 kg/ha), and covering pretreated straw (3-5 cm) after earthing;|[0071] the control group 1 is that NPK fertilizer (300 kg/ha) is evenly applied to the surface layer; |[0072] the control group 2 has the same fertilizing amount as the example group, but no functional bacterial liquid is added. |[0073] And (3) measuring carburetion efficiency, namely measuring the Total Organic Carbon (TOC) content of a soil sample by adopting a potassium dichromate oxidation-external heating method, air-drying, grinding and sieving (2 mm) the soil sample, oxidizing the organic carbon by using concentrated sulfuric acid and a potassium dichromate solution, and measuring the TOC content by a titration method. The water extract was filtered through a 0.45 μm filter, and the content of dissolved carbon (DOC) in the filtrate was measured by a total organic carbon analyzer, and the data are shown in table 1.|[0074] ;|[0075] Referring to Table1, the TOC of the example group was 25.3g/kg, the control group 1 was 18.7 g/kg, and the improvement was 35.3% (p < 0.05). The porous structure of the pyrolysis biochar adsorbs organic molecules, so that microbial decomposition is reduced, scanning electron microscopy verifies that pores are filled, the large-particle-size organic fertilizer is applied to deep soil, cultivation disturbance is reduced, and physical protection combination of the biochar and soil minerals is promoted. The TOC of the example group was significantly higher than that of control group 1, and the organic carbon storage in the soil was increased due to reduced decomposition of the organic carbon by adsorption of the biochar.|[0076] The DOC of the example group is 0.38 g/kg, the DOC of the control group 2 is 0.29 g/kg, and the improvement is 31.0%. Actinomycetes secrete Extracellular Polysaccharide (EPS), indicating that functional bacteria promote short-term retention of carbon.|[0077] An acidification inhibition assay; the pH value is measured by adopting a potentiometric method, a soil sample is naturally air-dried, filtered through a 2mm sieve, mixed with deionized water according to a mass ratio of 1:2.5, stirred for 30 minutes, and stood for 30 minutes, and the pH value of the suspension is measured by using a calibrated pH meter.|[0078] Determination of exchangeable acids by potassium chloride exchange methodAnd a hydrolyzable acidTaking air-dried soil sample 2.5 g with 2mm sieve, adding 1mol/LKCl solution 50 mL, oscillating for 2 hr, centrifuging to separate supernatant, and measuring exchange property by neutralization titrationConcentration (in cmol/kg);|[0079] Oxalic acid concentration was determined by High Performance Liquid Chromatography (HPLC). Subjecting the soil sample to methanol-water Extracting, centrifuging to obtain supernatant, purifying with C18 solid phase extraction column, concentrating, dissolving in mobile phase (0.1% formic acid water solution: acetonitrile=90:10), and quantifying oxalic acid concentration by HPLC (ultraviolet detector, lambda=210 nm), wherein the data are shown in Table 2.|[0080] ;|[0081] Referring to Table 2, the pH of the example group was 6.8, the pH of the control group 1 was 5.2, the elevation was 30.8% (p < 0.05), and the ash content generated by the thermal pyrolysis of biochar was rich、Neutralization of soil by ion exchange. Example group exchangeable acid 70.5% of control group 1, indicating that biochar was effective in reducing aluminum ionsAnd (5) dissolving out. The oxalic acid concentration of the example group was 12.3 mg/kg, the control group 2 was 22.1 mg/kg, and the reduction was 65.5% because the microorganism preferentially utilized the organic acid as the carbon source.|[0082] Anti-hardening experiment verification;|[0083] the hardening relief index measuring method comprises collecting original soil sample of 0-20 cm soil layers, and measuring volume The aluminum box is cut in layers to ensure the structural integrity of the soil, the fresh soil mass is weighed, recorded and then put into an oven (105 ℃) to be baked to constant weight for 48 hours, and the volume weight soil volume weight = dry soil mass (g)/annular cutter volume is calculated。|[0084] Taking an air-dried soil sample 20 g passing through a 2mm sieve, placing the air-dried soil sample into a settling cylinder, adding a 0.25 mm aperture sieve, injecting distilled water into the submerged soil, standing for 10 minutes, simulating the field moisture condition, slowly shaking the sieve, separating agglomerates, collecting fine particles passing through the sieve aperture, drying and weighing, and calculating the mass (g) of the agglomerates of more than 0.25 mm/the mass (g) of the total soil sample of more than 0.25 mm by 100 percent.|[0085] Placing undisturbed soil column with height of 10 cm and diameter of 10 cm in a permeameter, injecting distilled water into upper ring, keeping saturated state, collecting percolating water into lower ring, recording stable percolating time (about 30 min), and calculating water conductivity: Wherein Q is flow, L is soil column height, A is cross-sectional area, and h is head difference. The data are shown in Table 3. |[0086] ;|[0087] Referring to Table 3, the example set has a volume weight ofControl group 1 isThe drop is 20.7% (p < 0.05), and the granular structure is formed because the biochar fills the pores. The proportion of agglomerates in the example group greater than 0.25 mm is 50%, the proportion in the control group 2 is 42%, and the improvement is 19.0%. The water conductivity of the example group is 8.2 cm/h, the water conductivity of the control group 1 is 3.5 cm/h, and the improvement is 134%. The volume weight of the example group is reduced by 20.7% compared with that of the control group 1. Indicating that the decrease in permeability due to hardening is improved.|[0088] It should be understood that the foregoing is by way of example only and is not intended to limit the embodiments. Other variations and modifications of the present invention will be apparent to those of ordinary skill in the art in light of the foregoing description. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present invention.|[0089] In the description of the present invention, it should be understood that the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.|[0090] In the description of this specification, the terms "one," "some," "examples," "specific examples," or "some examples," etc., refer to a particular feature, structure, material, or characteristic described in connection with the or an example as being included in at least one or an example of the invention. In this specification, schematic representations of the above terms are not necessarily for the same example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more or examples. Furthermore, the different examples described in this specification and the features of the different examples may be combined and combined by those skilled in the art without contradiction.|[0091] It will be appreciated that the foregoing is illustrative and is not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made therein by those skilled in the art within the scope of the invention. Family Number|(115835752)|115835752|Abstract|(CN120548812B B)|The invention relates to the technical field of soil function improvement , in particular to a rice field soil recarburization and capacity expansion method based on a charcoal - based organic fertilizer . The method comprises the following steps : crushing a biomass raw material , pyrolyzing and cooling to obtain biochar ; immersing the biochar in a functional bacteria solution containing actinomycetes and bacillus for activating treatment to obtain modified biochar ; mixing the modified biochar and decomposed straw , composting and fermenting to obtain organic fertilizers with different particle sizes ; the large - particle - size organic fertilizer is applied to deep soil , the soil is covered with soil after straw is laid on the soil , and the small - particle - size organic fertilizer is applied to surface soil . Through layered application , the large - particle - size biochar repairs the deep soil structure and expands the carbon storage capacity , and meanwhile , the carbon stability is improved through carbon - nitrogen synergistic metabolism driven by functional bacteria , so that the carbon immobilization efficiency is improved , meanwhile , soil recarburization and expansion are achieved , the contradiction between carbon sequestration and structure degradation and nutrient imbalance in a traditional recarburization and expansion technology is solved , and the soil recarburization and expansion efficiency is improved . Synergic improvement of a carbon sink function and agricultural productivity is promoted . |CPC codes|(CN120548812B B)|A01B - 079/00 |A01B - 079/02 |IPC codes|(CN120548812B B)|A01B - 079/00 |A01B - 079/02 | Basic materials chemistry|Other special machines A01B-079/02|C05D-009/00|C05F-003/00|C05F-011/00|C05F-011/08|C05F-017/00|C05G-003/80|Y02W-030/43 (GR1) C05D-009/00[RK1]; C05F-009/04[RK2]; C05F-011/08[RK3]; C05F-017/20[RK4]; C05F-017/50[RK5]; C05G-003/80[RK6]; C05G-005/12[RK7] A01B-079/02|C05D-009/00|C05F-003/00|C05F-011/00|C05F-011/08|C05F-017/00|C05G-003/80|Y02W-030/43 A01B-079/00|A01B-079/02|C05F-017/20|C05F-017/50|C05G-003/80|C05G-005/12 A01B-079/00|A01B-079/02|C05F-017/20|C05F-017/50|C05G-003/80|C05G-005/12 CN120858687|CN120987681B CN120858687 116501709 WHO=Examiner SELF=Y CAT=A|CN120987681B 116764767 WHO=Examiner SELF=N CN120359862|CN115259920|AU2020101136|CN108658704|CN107285964|CN107512974|US20180009720|CN105418273|CN111116273 CN120359862 115427115 WHO=Examiner SELF=N CAT=A|CN115259920 102359628 WHO=Examiner SELF=Y CAT=A|AU2020101136 89962682 WHO=Examiner SELF=N CAT=A|CN108658704 81644149 WHO=Examiner SELF=N CAT=A|CN107285964 77572143 WHO=Examiner SELF=N CAT=A|CN107512974 78182835 WHO=Examiner SELF=N CAT=A|US20180009720 78300542 WHO=Examiner SELF=N CAT=A|CN105418273 72468805 WHO=Examiner SELF=N CAT=A|CN111116273 88680259 WHO=Examiner SELF=N CN107512974; CN108658704; AU2020101136; CN115259920; CN120359862; CN105418273; CN107285964; US20180009720; CN111116273 GRANTED (CN120548812)|GRANTED ALIVE (CN120548812)|ALIVE (CN120548812)|LEGAL DETAILS FOR CN120548812|Actual or expected expiration date=2045-07-30|Legal state=ALIVE|Status=GRANTED|Event publication date=2025-07-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511056627|Application date=2025-07-30|Standardized application number=2025CN-1056627|Event publication date=2025-08-29|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120548812|Publication stage code=A|Publication date=2025-08-29|Standardized publication number=CN120548812|Event publication date=2025-08-29|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-09-16|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-10-03|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN120548812|Publication stage code=B|Publication date=2025-10-03|Standardized publication number=CN120548812B|Event publication date=2025-10-03|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN120548812)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfeHw0wRAiOJxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000079231282&ekey=2269&xpn=CN120548812B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=xOVTl7sr%252F0hmmrw3lS7v9rmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN120548812)|CN|(CN120548812)|CN (CN120548812)|NAME=NORTHEAST INSTITUTE OF GEOGRAPHY & AGROECOLOGY CHINESE ACADEMY OF SCIENCES , COUNTRY=CN|(CN120548812)|NAME=NORTHEAST INSTITUTE OF GEOGRAPHY & AGROECOLOGY CHINESE ACADEMY OF SCIENCES , COUNTRY=CN (CN120548812)|NAME=QIU YU;Shenyang Hongmai Intellectual Property Agency (General Partnership) , REG=21274|(CN120548812)|NAME=QIU YU;Shenyang Hongmai Intellectual Property Agency (General Partnership) , REG=21274 (CN120548812)|CN|(CN120548812)|CN (CN120548812)|NAME=WANG WEIQI, COUNTRY=CN |NAME=ZHANG HAO|NAME=ZOU YUANCHUN|NAME=LIANG YAO|NAME=LIANG SHUANG|(CN120548812)|NAME=WANG WEIQI, COUNTRY=CN |NAME=ZHANG HAO|NAME=ZOU YUANCHUN|NAME=LIANG YAO|NAME=LIANG SHUANG 0 1 Titre: (CN120548812)|Rice field soil carburetion and capacity expansion method based on biochar-based organic fertilizer Résumé: (CN120548812)|The invention relates to the technical field of soil function improvement, in particular to a rice field soil recarburization and capacity expansion method based on a charcoal-based organic fertilizer. The method comprises the following steps: crushing a biomass raw material, pyrolyzing and cooling to obtain biochar; immersing the biochar in a functional bacteria solution containing actinomycetes and bacillus for activating treatment to obtain modified biochar; mixing the modified biochar and decomposed straw, composting and fermenting to obtain organic fertilizers with different particle sizes; the large-particle-size organic fertilizer is applied to deep soil, the soil is covered with soil after straw is laid on the soil, and the small-particle-size organic fertilizer is applied to surface soil. Through layered application, the large-particle-size biochar repairs the deep soil structure and expands the carbon storage capacity, and meanwhile, the carbon stability is improved through carbon-nitrogen synergistic metabolism driven by functional bacteria, so that the carbon immobilization efficiency is improved, meanwhile, soil recarburization and expansion are achieved, the contradiction between carbon sequestration and structure degradation and nutrient imbalance in a traditional recarburization and expansion technology is solved, and the soil recarburization and expansion efficiency is improved. Synergic improvement of a carbon sink function and agricultural productivity is promoted. 86 Abstract gpt-4o-mini no The article focuses on soil improvement and carbon storage using biochar and does not explicitly address accelerated weathering or CO₂ capture through mineral alteration.
87 US63/460,553P|US63/599,946P|US63/557,387P WOUS2024/025537 WO2024/220896|WO2024/220896 111908782 WO2024/220896 A3 2025-01-23 [WO2024220896]|WO2024/220896 A2 2024-10-24 [WO2024220896] 2023-04-19|2023-11-16|2024-02-23 2024-04-19 2025-01-23|2024-10-24 (WO2024/220896)|2026-10-19 (WO2024/220896)|Carbon dioxide removal with biochar fortified by accelerated weathering of basalt (abfb) (WO2024/220896)|Embodiments of the present disclosure pertain to a composition that includes at least one basalt and at least one biochar. The biochai- may include nutrient fortified biochar, where the nutrients are derived from the basalt. Additional embodiments of the present disclosure pertain to methods of capturing CO2 from an environment by exposing the environment to a composition of the present disclosure. The compositions of the present disclosure may also enhance the nutrient content of the environment. Further embodiments of the present disclosure pertain to methods of enhancing soil fertility by applying a composition of the present disclosure to the soil. Additional embodiments pertain to methods of making a composition by altering at least one basalt and mixing the altered basalt with at least one biochar. DARTMOUTH COLLEGE (WO2024/220896)|TRUSTEES OF DARTMOUTH COLLEGE ([US])|(WO2024/220896)|TRUSTEES OF DARTMOUTH COLLEGE ([US]) SHARMA MUKUL (WO2024/220896)|SHARMA, Mukul|(WO2024/220896)|SHARMA, Mukul (WO2024/220896)|AMINI, Farhang ([US]) (WO2024/220896)|For instance, in some embodiments, exposure of the compositions of the present disclosure to an environment result in the enhancement of Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, and/or N in the environment. [0059] The enhancement of the nutrient content of environments can have various advantageous effects.|In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, and/or N. [0068] The methods of the present disclosure may have various advantages.|PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0025] As such, a need exists for more effective and less hazardous materials for CDR.| (WO2024/220896)|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises: at least one biochar; and at least one basalt.|12. A method of enhancing soil fertility, wherein the method comprises applying a composition to the soil, wherein the composition comprises: at least one biochar; and at least one basalt.|20. A method of making a composition, said method comprising: altering at least one basalt; and mixing the altered basalt with at least one biochar.|41. A composition comprising: at least one basalt; and at least one biochar, wherein the biochar comprises nutrient fortified biochar, and wherein the nutrients are derived from the basalt.| (WO2024/220896)|Embodiments of the present disclosure pertain to a composition that includes at least one basalt and at least one biochar. The biochai- may include nutrient fortified biochar, where the nutrients are derived from the basalt.| (WO2024/220896)|BIOCHAR(100,3)|ACCELERATED WEATHERING(100,1)|BASALT ACCELERATED WEATHERING(100,1)|CARBON DIOXIDE(100,1)|CARBON DIOXIDE REMOVAL(100,1)|BASALT(32,3)|SOIL FERTILITY ENHANCEMENT(31,2)|CAPTURING CO2(29,2)|NUTRIENT(27,2)||(WO2024/220896)|BIOCHAR(100,3)|ACCELERATED WEATHERING(100,1)|BASALT ACCELERATED WEATHERING(100,1)|CARBON DIOXIDE(100,1)|CARBON DIOXIDE REMOVAL(100,1)|BASALT(32,3)|SOIL FERTILITY ENHANCEMENT(31,2)|CAPTURING CO2(29,2)|NUTRIENT(27,2)| (WO2024/220896)|PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 CLAIMS |1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises: at least one biochar; and at least one basalt.|2. The method of claim 1, wherein the environment is selected from the group consisting of an airstream, a gas stream, an industrial plant, an atmosphere, ambient air, a water source, soil, or combinations thereof.|3. The method of claim 1, wherein the composition also enhances the nutrient content of the environment.|4. The method of claim 1, wherein the environment comprises soil, and wherein the composition also enhances the fertility of the soil.|5. The method of claim 4, wherein the soil is part of a field, wherein the field is selected from the group consisting of an agricultural field, a residential field, a cropland, a park, a subdivision, a yard, a highway, a sports facility, a golf course, or combinations thereof.|6. The method of claim 1, wherein the biochar comprises nutrient fortified biochar, wherein the nutrients are derived from the basalt.|PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 |7. The method of claim 6, wherein the nutrients are selected from the group consisting of Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof.|8. The method of claim 1, wherein the basalt comprises altered basalt.|9. The method of claim 8, wherein the altered basalt comprises powdered basalt.|10. The method of claim 8, wherein the altered basalt comprises heated basalt.|11. The method of claim 1, wherein the composition comprises altered basalt and nutrient fortified biochar (ABFB), wherein the nutrients are derived from the basalt.|12. A method of enhancing soil fertility, wherein the method comprises applying a composition to the soil, wherein the composition comprises: at least one biochar; and at least one basalt.|13. The method of claim 12, wherein the soil is part of a field, wherein the field is selected from the group consisting of an agricultural field, a residential field, a cropland, a park, a subdivision, a yard, a highway, a sports facility, a golf course, or combinations thereof.|14. The method of claim 12, wherein the biochar comprises nutrient fortified biochar, wherein the nutrients are derived from the basalt.|PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 |15. The method of claim 14, wherein the nutrients are selected from the group consisting of Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof.|16. The method of claim 12, wherein the basalt comprises altered basalt.|17. The method of claim 16, wherein the altered basalt comprises powdered basalt.|18. The method of claim 16, wherein the altered basalt comprises heated basalt.|19. The method of claim 12, wherein the composition comprises altered basalt and nutrient fortified biochar (ABFB), wherein the nutrients are derived from the basalt.|20. A method of making a composition, said method comprising: altering at least one basalt; and mixing the altered basalt with at least one biochar.|21. The method of claim 20, wherein the altering comprises heating the basalt.|22. The method of claim 21, wherein the heating occurs at a temperature of at least 100 °C.|PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 |23. The method of claim 21, wherein the heating occurs under acidic conditions.|24. The method of claim 20, wherein the altering comprises grinding the basalt to form a powder.|25. The method of claim 20, wherein the mixing comprises homogenization.|26. The method of claim 20, wherein the mixing occurs under alkaline conditions.|27. The method of claim 20, wherein the method results in nutrient fortification of the biochar, wherein the nutrients are derived from the altered basalt.|28. The method of claim 27, wherein the nutrients are selected from the group consisting of Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof.|29. The method of claim 20, further comprising a step of forming the biochar from biomass.|30. The method of claim 29, wherein the biochar formation comprises heating the biomass through pyrolysis.|31. The method of claim 29, wherein the method prevents the release of carbon dioxide (CO2) from the biomass.|PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 |32. The method of claim 29, wherein the method comprises: forming the biochar, wherein the forming comprises placing a biomass in a gasifier associated with an engine operable to generate electricity and/or steam, wherein the gasifier produces biochar and syngas, and wherein the engine generates electricity and/or steam from the syngas; altering the basalt, wherein altering is powered by the electricity and/or steam generated from the engine; and mixing the altered basalt with the produced biochar to form the composition.|33. The method of claim 32, wherein the engine generates steam, and wherein the generated steam from the engine powers the altering of the basalt.|34. The method of claim 32, wherein the engine generates electricity, and wherein the generated electricity from the engine powers the altering of the basalt.|35. The method of claim 32, wherein the altering comprises heating the basalt in a reactor.|36. The method of claim 35, wherein the heating occurs at a temperature of at least 100 °C under acidic conditions.|PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 |37. The method of claim 35, wherein the engine also generates steam, wherein the steam is utilized to heat the basalt in a reactor.|38. The method of claim 32, wherein the altering comprises grinding the basalt to form a powder.|39. The method of claim 32, wherein the gasifier produces biochar through pyrolysis.|40. The method of claim 20, wherein the method is used to capture CO2 from an environment during the production of the composition.|41. A composition comprising: at least one basalt; and at least one biochar, wherein the biochar comprises nutrient fortified biochar, and wherein the nutrients are derived from the basalt.|42. The composition of claim 41, wherein the nutrients are selected from the group consisting of Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof.|43. The composition of claim 41, wherein the basalt comprises altered basalt.|44. The composition of claim 43, wherein the altered basalt comprises powdered basalt.|PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 |45. The composition of claim 43, wherein the altered basalt comprises heated basalt.|46. The composition of claim 45, wherein the heated basalt is heated under acidic conditions.|47. The composition of claim 41, wherein the composition is in homogenized form. (WO2024/220896)|[0001] PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-03 TITLE CARBON DIOXIDE REMOVAL WITH BIOCHAR FORTIFIED BY ACCELERATED WEATHERING OF BASALT (ABFB) CROSS-REFERENCE TO RELATED APPLICATIONS [0001] This application claims priority to U.S. Provisional Patent Application No.63/460,553, filed on April 19, 2023; U.S. Provisional Patent Application No.63/599,946, filed on November 16, 2023; and U.S. Provisional Patent Application No.63/557,387, filed on February 23, 2024. The entirety of each of the aforementioned applications is incorporated herein by reference. BACKGROUND [0002] Current methods and compositions for capturing carbon dioxide from environments have numerous limitations. Embodiments of the present disclosure aim to address the aforementioned limitations. SUMMARY [0003] In some embodiments, the present disclosure pertains to a composition that includes at least one basalt and at least one biochar. In some embodiments, the biochar includes nutrient fortified biochar. In some embodiments, the nutrients are derived from the basalt. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof. [0004] In some embodiments, the basalt in the compositions of the present disclosure include altered basalt. In some embodiments, the altered basalt includes powdered basalt, heated basalt, or combinations thereof. [0005] Additional embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure. In some embodiments, the compositions of the present disclosure also enhance the nutrient content of the environment. For instance, in some embodiments where the environment includes soil, the compositions of the present disclosure also enhance the fertility of the soil. Additional embodiments of the present disclosure pertain to methods of enhancing soil fertility by applying a composition of the present disclosure to the soil.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0006] Further embodiments of the present disclosure pertain to methods of making a composition by altering at least one basalt and mixing the altered basalt with at least one biochar. In some embodiments, the altering occurs by heating the basalt under acidic conditions. In some embodiments, the altering includes grinding the basalt to form a powder. [0007] In some embodiments, the mixing of altered basalt with biochar results in nutrient fortification of the biochar by the nutrients derived from the altered basalt. In some embodiments, the methods of the present disclosure also include a step of forming the biochar. In some embodiments, biochar formation occurs by heating a biomass, such as through pyrolysis. In some embodiments, the methods of the present disclosure may also be utilized to prevent the release of carbon dioxide (CO2) from the biomass during biochar production. [0008] In some embodiments, the methods of the present disclosure occur through the following steps: (1) forming the biochar, where the forming includes placing a biomass in a gasifier associated with an engine operable to generate electricity and/or steam, where the gasifier produces biochar and syngas, and where the engine generates electricity and/or steam from the syngas; (2) altering the basalt by utilizing the electricity and/or steam generated from the engine; and (3) mixing the altered basalt with the produced biochar to form the composition. In some embodiments, the engines of the present disclosure may generate steam (e.g., hot water). In some embodiments, the steam (e.g., hot water) generated from an engine may be utilized to alter the basalt. In some embodiments, the engines of the present disclosure may generate electricity. In some embodiments, the electricity generated from the engine may be utilized to alter the basalt. DRAWINGS [0009] FIG. 1A illustrates a method capturing carbon dioxide (CO2) from an environment in accordance with various embodiments of the present disclosure. [0010] FIG.1B illustrates a method of enhancing soil fertility in a subject in accordance with various embodiments of the present disclosure. [0011] FIG. 1C illustrates a method of making a basalt-biochar composition in accordance with various embodiments of the present disclosure.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0012] FIG. 1D provides a diagram of a system for making a basalt-biochar composition in accordance with various embodiments of the present disclosure. [0013] FIG. 1E illustrates an alternative method of making a basalt-biochar composition in accordance with various embodiments of the present disclosure. [0014] FIGS.2A-2B provide experimental results demonstrating that the basalt-biochar compositions of the present disclosure enhance soil fertility. [0015] FIGS.3-4 illustrate schemes for the production of altered basalt with fortified biochar (ABFB) using electricity generated from syngas, where the syngas is produced by a biochar producing gasifier. [0016] FIGS. 5-7 illustrate additional processes of forming ABFB in accordance with various embodiments of the present disclosure. [0017] FIG. 8 shows an image of an ABFB formed in accordance with the methods of the present disclosure. DETAILED DESCRIPTION [0018] It is to be understood that both the foregoing general description and the following detailed description are illustrative and explanatory, and are not restrictive of the subject matter, as claimed. In this application, the use of the singular includes the plural, the word “a” or “an” means “at least one”, and the use of “or” means “and/or”, unless specifically stated otherwise. Furthermore, the use of the term “including”, as well as other forms, such as “includes” and “included”, is not limiting. Also, terms such as “element” or “component” encompass both elements or components comprising one unit and elements or components that include more than one unit unless specifically stated otherwise. [0019] The section headings used herein are for organizational purposes and are not to be construed as limiting the subject matter described. All documents, or portions of documents, cited in this application, including, but not limited to, patents, patent applications, articles, books, and treatises, are hereby expressly incorporated herein by reference in their entirety for any purpose. In the event that one or more of the incorporated literature and similar materials defines a term in a manner that contradicts the definition of that term in this application, this application controls.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0020] Carbon dioxide (CO2) removal (CDR) is a key process for addressing climate change. There are two prominent CDR strategies for addressing climate change: enhanced silicate rock weathering (EW) (Beerling et al., 2024, Beerling et al., 2020, Beerling et al., 2018, Taylor et al., 2016, Lewis et al., 2021, Schuiling and Krijgsman, 2006) and application of biochar (Kambo and Dutta, 2015, Lehmann et al., 2015, Lehmann et al., 2021, Rodriguez Franco et al., 2024, Woolf et al., 2010, Xia et al., 2023, Xiao et al., 2018, Amonette et al., 2021, Lehmann, 2007, Schmidt et al., 2011). However, both strategies have significant drawbacks. [0021] In particular, the EW strategy involves crushing basalt to a fine powder to speed-up weathering reactions. This strategy, however, still suffers from slow reaction kinetics (Strefler et al., 2018). For instance, to remove 1 Pg C per year would require about 21 Pg of basalt to be mined, ground to 20 μm, and spread on croplands every year. [0022] Use of biochar is yet another strategy for CDR (Lehmann et al., 2021, Shrestha et al., 2023). Preparation of biochar involves heating biomass (e.g., wood and/or crop residues) in an airless oven at temperatures ranging from 300 °C to 800 °C. Biochar carbon should be stable in soil for over centuries to be of value for long-term CDR (Lehmann et al., 2015). In fact, it has been shown that biochar prepared at 600 °C or higher is especially recalcitrant (Lehmann et al., 2021). Oxidative resistance and occlusion by clay minerals may combine to make biochar (Mašek et al., 2019, Rawal et al., 2016, Yang et al., 2018) persist in soil for hundreds of years. [0023] Adapting biochar globally as a soil amendment can affect both CDR and greenhouse gas emissions (Lehmann et al., 2021). However, several studies have shown that organic pollutants (e.g., polycyclic aromatic hydrocarbons (PAHs)) are synthesized during biochar preparation (Godlewska et al., 2021, Hale et al., 2012, Kołtowski and Oleszczuk, 2015, Odinga et al., 2021). These pollutants can remain in the soil, making its application to croplands questionable (Rombolà et al., 2019, Shepherd et al., 2017a). [0024] Furthermore, preparation of biochar also releases roughly similar amounts of liquid and gaseous CO2 (CO2e) thereby reducing CDR efficiency by a factor of about 1.9. In particular, for every ton of biochar produced, about 0.74 ton of CO2e (gases and liquids) is released (Crombie and Mašek, 2015).PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0025] As such, a need exists for more effective and less hazardous materials for CDR. A need also exists for safer and more effective methods of mass producing such materials. Numerous embodiments of the present disclosure aim to address the aforementioned needs. [0026] Compositions [0027] In some embodiments, the present disclosure pertains to a composition. In some embodiments, the composition includes at least one biochar and at least one basalt. In some embodiments, the biochar and basalt are associated with one another. As set forth in more detail herein, the compositions of the present disclosure can include various basalts and biochars in various arrangements. [0028] Biochar [0029] Biochar generally refers to a condensed aromatic carbon rich substance that forms when biomass (e.g., wood and/or crop residues) is heated in a container at a high temperature (e.g., temperatures ranging from 300 °C to 800 °C with little or no available oxygen (i.e., pyrolysis)). The compositions of the present disclosure can include various types of biochar. For instance, in some embodiments, the biochar includes alkaline biochar. In some embodiments, the biochar includes corn husk biochar. In some embodiments, the biochar includes nutrient fortified biochar. In some embodiments, the nutrients are derived from the basalt. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof. [0030] Basalts [0031] Basalt generally refers to a mafic aphanitic volcanic rock that includes, without limitation, tholeiites (Best, 2013, Cox et al., 1979, Hughes, 2013, Wilson, 1989, Winter, 2014, Carmichael et al., 1974). Basalt is exposed around the world on the continents and at the ocean floor. [0032] The composition of the present disclosure can also include various types of basalts. For instance, in some embodiments, the basalts include, without limitation, plagioclase feldspars- containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. In some embodiments, the basalts contain, without limitation, plagioclase feldspars-pyroxenes, with or without any olivine.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0033] In some embodiments, basalts in the compositions of the present disclosure include plagioclase feldspars-containing basalts and pyroxenes-containing basalts. In some embodiments, basalts in the compositions of the present disclosure include microscopic or visible plagioclase feldspars-containing basalts and pyroxenes-containing basalts, with little or no olivines, and with minor iron spinel and phosphate. [0034] The basalts in the compositions of the present disclosure could be from several basalt regions around the world and/or from various localities. For instance, in some embodiments, the basalts in the compositions of the present disclosure may include Holyoke Basalt (MA) and Butner Basalt (NC), which belong to Central Atlantic Magmatic Province that is exposed along the US Eastern Seaboard, Columbia River Flood Basalt, Deccan Traps, Karoo Basalts, Parana Basalts, Siberian Traps, Hawaiian Basalts, Icelandic Basalts, or other regions. [0035] In some embodiments, the basalts in the compositions of the present disclosure include tholeiites. In some embodiments, the basalts in the compositions of the present disclosure include tholeiites with low heavy metal concentrations. [0036] In some embodiments, the basalts in the compositions of the present disclosure include Holyoke Basalt. In some embodiments, the basalts in the compositions of the present disclosure include Deccan Basalt. [0037] In some embodiments, the basalts in the compositions of the present disclosure have been naturally altered. In some embodiments, the basalts in the compositions of the present disclosure are in isolated form (i.e., basalt isolated from its native environment, such as through mining). In some embodiments, the basalts in the compositions of the present disclosure include mined basalt. In some embodiments, the basalts in the compositions of the present disclosure include basalt that have been crushed and ground to a range of grain-sizes. In some embodiments, the basalts in the compositions of the present disclosure include basalt that have been partially altered to clay minerals.| [0002] PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0038] In some embodiments, the basalts in the basalts in the compositions of the present disclosure include altered basalt. In some embodiments, the altered basalt is in powdered form. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 1 mm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 800 µm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 500 µm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 100 µm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 50 µm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 20 µm. [0039] In some embodiments, the powdered basalt may be in the form of particles. In some embodiments, the powdered basalt particles may be in the form of coarse particles, medium particles, coarse-grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. [0040] In some embodiments, the altered basalt includes heated basalt. In some embodiments, the heated basalt is heated at a temperature of at least 100 °C. In some embodiments, the heated basalt is heated at a temperature of at least 150 °C. In some embodiments, the heated basalt is heated at a temperature of at least 200 °C. In some embodiments, the heated basalt is heated under acidic conditions. [0041] Composition forms [0042] The compositions of the present disclosure may be in various forms. For instance, in some embodiments, the compositions of the present disclosure include altered basalt. In some embodiments, the compositions of the present disclosure include biochar that has been fortified with nutrients from altered basalt (ABFB). In some embodiments, the nutrients are derived from altered basalt. In some embodiments, the nutrients are derived from altered basalt and from biochar. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, N, salts thereof, oxides thereof, or combinations thereof.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0043] The ABFBs of the present disclosure can include various ratios of biochar and altered basalt. For instance, in some embodiments, the biochar: altered basalt ratio could vary from 0 to 0.25. In some embodiments, the biochar: altered basalt ratio could vary from 0 to 0.5. In some embodiments, the biochar: altered basalt ratio could vary from 0 to 0.75. In some embodiments, the biochar: altered basalt ratio could vary from 0 to 1.0. In some embodiments, the biochar: altered basalt ratio is about 0.25. In some embodiments, the biochar: altered basalt ratio is about 0.5. In some embodiments, the biochar: altered basalt ratio is about 0.75. In some embodiments, the biochar: altered basalt ratio is about 1. [0044] In some embodiments, the compositions of the present disclosure are in the form of a slurry. In some embodiments, the compositions of the present disclosure are in homogenized form. In some embodiments, the compositions of the present disclosure include organo-clay complexes, organo-Fe- oxyhydroxide complexes, or combinations thereof. [0045] Methods of capturing carbon dioxide (CO2) from an environment [0046] Additional embodiments of the present disclosure pertain to a method of capturing carbon dioxide (CO2) from an environment. In some embodiments illustrated in FIG.1A, the methods of the present disclosure include exposing the environment to a composition of the present disclosure (step 10) to result in the capture of the CO2 form the environment (step 12). In some embodiments, the compositions of the present disclosure also enhance the nutrient content of the environment (step 14). As set forth in more detail herein, the methods of the present disclosure can be utilized to capture various types of CO2 from various environments. [0047] Carbon dioxide (CO2) [0048] The method of the present disclosure may be utilized to capture various types of CO2. For instance, in some embodiments, the CO2 to be captured include, without limitation, carbon dioxide CO2 from air, soil and/or water. [0049] Without being bound by theory, the capture of CO2 by the compositions of the present disclosure can occur through various mechanisms. For instance, in some embodiments, the capturing of the CO2 occurs by a method that includes, without limitation, dissolution, pyrolysis, adhesion, binding, adsorption, electrostatic interaction, or combinations thereof. [0050] Exposure of environment to a compositionPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0051] The methods of the present disclosure may be utilized to capture CO2 from various environments. For instance, in some embodiments, the environment includes, without limitation, an airstream, a gas stream, an industrial plant, an atmosphere, ambient air, a water source, soil, or combinations thereof. In some embodiments, the environment includes ambient air. In some embodiments, the environment includes an atmosphere. [0052] In some embodiments, the environment includes a water source. In some embodiments, the water source includes, without limitation, a body of water, an ocean, a sea, a lake, a pond, or combinations thereof. In some embodiments, the water source includes a sea. In some embodiments, the water source includes an ocean. [0053] In some embodiments, the environment includes soil. In some embodiments, the soil is part of a field. In some embodiments, the field includes, without limitation, an agricultural field, a residential field, a cropland, a park, a subdivision, a yard, a highway, a sports facility, a golf course, or combinations thereof. [0054] The compositions of the present disclosure may be exposed to an environment in various manners. For instance, in some embodiments, the exposing occurs by flowing the environment through the composition. In some embodiments, the exposing occurs by placing the composition at or near the environment. [0055] In some embodiments, the exposing of an environment to a composition of the present disclosure occurs by a method that includes, without limitation, incubating, spreading, pouring, sprinkling, spraying, or combinations thereof. In some embodiments where the environment includes soil, the compositions of the present disclosure may be exposed to the soil by sprinkling the composition onto the soil. [0056] Desirable levels of soil organic carbon below which crop yield declines may be ~2% in soils of the temperate zone and ~1% for those of the tropics (Lal, 2020). Soils with organic carbon contents exceeding 5% are highly fertile (Lal, 2020). In some embodiments, the compositions of the present disclosure (e.g., ABFBs) can be used to boost soil organic carbon content. Depending on their compositions, the compositions of the present disclosure (e.g., ABFBs) can be deployed on cropland and degraded soils such that they reach or exceed a desirable level in a single application of ABFB. [0057] Enhancement of nutrient content of environmentPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0058] In some embodiments, the compositions of the present disclosure also enhance the nutrient content of the environment. For instance, in some embodiments, exposure of the compositions of the present disclosure to an environment result in the enhancement of Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, and/or N in the environment. [0059] The enhancement of the nutrient content of environments can have various advantageous effects. For instance, in some embodiments where the environment includes soil, the compositions of the present disclosure may enhance soil fertility. [0060] Methods of enhancing soil fertility [0061] Additional embodiments of the present disclosure pertain to a method of enhancing soil fertility. In some embodiments illustrated in FIG.1B, the methods of the present disclosure include exposing the soil to a composition of the present disclosure (step 16) to result in the enhancement of the soil’s fertility (step 18). [0062] Exposure of soil to a composition [0063] The compositions of the present disclosure may be exposed to soil in various manners. For instance, in some embodiments, the exposing of a soil to a composition of the present disclosure occurs by a method that includes, without limitation, incubating, spreading, pouring, sprinkling, spraying, or combinations thereof. In some embodiments, exposing of a soil to a composition of the present disclosure occurs by sprinkling the composition onto the soil. In some embodiments, exposing of a soil to a composition of the present disclosure occurs by spraying the composition onto the soil. [0064] Soils [0065] The compositions of the present disclosure may be applied to various types of soils. For instance, in some embodiments, the soil is part of a field. In some embodiments, the field includes, without limitation, an agricultural field, a residential field, a cropland, a park, a subdivision, a yard, a highway, a sports facility, a golf course, or combinations thereof. [0066] Enhancement of soil fertilityPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0067] Without being bound by theory, the compositions of the present disclosure may enhance a soil’s fertility in various manners. For instance, in some embodiments, the compositions of the present disclosure enhance soil fertility by at least providing nutrients to the soil, decreasing soil acidity, increasing soil carbon content, increasing soil water content, or combinations thereof. In some embodiments, the compositions of the present disclosure enhance soil fertility by at least providing nutrients to the soil. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, and/or N. [0068] The methods of the present disclosure may have various advantages. For instance, in some embodiments, the methods of the present disclosure may be utilized to enhance food security, reduce energy poverty, and address climate change. [0069] Methods of making compositions [0070] Additional embodiments pertain to a method of making the compositions of the present disclosure. In some embodiments, the method includes mixing at least one biochar with at least one basalt to form the compositions of the present disclosure. [0071] The methods of the present disclosure may be utilized to mix various types of basalts and biochars. Suitable basalts and biochars were described supra and are incorporated herein by reference. As set forth in more detail, the methods of the present disclosure can occur through various processes. [0072] Altering basalts [0073] In some embodiments, the methods of the present disclosure also include a step of altering a basalt. In some embodiments, the altering occurs prior to mixing the basalt with the biochar. [0074] Basalts may be altered through various processes. For instance, in some embodiments, altering includes grinding the basalt. In some embodiments, the altering results in the formation of a basalt powder. [0075] In some embodiments, the altering includes heating the basalt. In some embodiments, the heating occurs at a temperature of at least 100 °C. In some embodiments, the heating occurs at a temperature of at least 150 °C. In some embodiments, the heating occurs at a temperature of at least 200 °C.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0076] In some embodiments, basalts are heated under acidic conditions. For instance, in some embodiments, basalt may be heated in an acidic solution. In some embodiments, the acidic solution includes, without limitation, an acetic acid solution, a carbonic acid solution, a vinegar solution, a wood vinegar solution, a citric acid solution, an oxalic acid solution, a pyroligneous acid solution, or combinations thereof. In some embodiments, the heating occurs in an acidic solution at a temperature of at least 100 °C and a pH of less than 7. [0077] Forming biochar [0078] In some embodiments, the methods of the present disclosure also include a step of forming the biochar. Various methods may be utilized to form biochar. For instance, in some embodiments, biochar is formed by heating biomass. In some embodiments, the heating includes pyrolysis of the biomass. In some embodiments, heating occurs at a temperature of at least 300 °C. In some embodiments, the heating occurs at a temperature of at least 400 °C. In some embodiments, the heating occurs at a temperature of at least 500 °C. In some embodiments, the heating occurs at a temperature ranging from about 300 °C to about 800 °C. [0079] Biochars may be formed from various biomasses. For instance, in some embodiments, the biomass includes, without limitation, walnut shells, wood residues, hardwood chips, softwood chips, wood shavings, crop residues, or combinations thereof. [0080] In some embodiments, the methods of the present disclosure also involve preventing the emission of carbon dioxide (CO2) from biomass. It is widely understood that plants absorb CO2 during photosynthesis, transforming it into various organic compounds such as cellulose, hemicellulose, and/or lignin. Upon the plant's demise, this biomass undergoes remineralization, releasing CO2 back into the atmosphere. The creation of biochar from biomass has the potential to impede the process of remineralization, thereby preventing the conversion of carbon fixed during photosynthesis into CO2. [0081] Mixing of basalt and biocharPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0082] The methods of the present disclosure can utilize various processes to mix basalts and biochars. For instance, in some embodiments, the mixing includes homogenization. In some embodiments, the mixing occurs under alkaline conditions. In some embodiments, the mixing occurs at a pH of at least 7. In some embodiments, the mixing occurs at a pH of at least 7.5. [0083] In some embodiments, the mixing occurs above room temperature. For instance, in some embodiments, the mixing occurs at a temperature of 100 °C or higher. In some embodiments, the mixing occurs at a temperature of 120 °C or higher. In some embodiments, the mixing occurs at a temperature of 120 °C or higher. In some embodiments, the mixing occurs at a temperature of about 200 °C. [0084] In some embodiments, basalts may be mixed with biochars after being altered. For instance, in some embodiments illustrated in FIG. 1C, the methods of the present disclosure may include: altering the basalt (step 20) and mixing the altered basalt with biochar (step 22) to form a composition of the present disclosure (step 24). In some embodiments, the methods of the present disclosure also include a step of forming biochar (step 21) and then mixing the formed biochar with the altered basalt (step 22). [0085] Mixing biochars with basalts can have various effects. For instance, in some embodiments, the method results in nutrient fortification of the biochar. In some embodiments, the nutrients are derived from the basalt. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof. In some embodiments, the method results in the association of one or more organic materials with the altered basalt. [0086] The methods of the present disclosure can be utilized to form various types of compositions. Suitable compositions were described supra and are incorporated herein by reference. For instance, in some embodiments, the formed composition has a pH of more than 7. In some embodiments, the alkaline pH provides a negative surface charge, thereby allowing sorption of various materials (e.g., cations and organic moieties) onto the altered basalt and biochar. In some embodiments, the formed composition includes organo-clay complexes, organo-Fe-oxyhydroxide complexes, or combinations thereof. [0087] Systems for the formation of compositionsPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0088] The compositions of the present disclosure may be formed through the utilization of various systems. Additional embodiments of the present disclosure pertain to such systems for the formation of the compositions of the present disclosure. With reference to system 50 in FIG.1D for illustrative purposes, the systems of the present disclosure may include a gasifier 52 associated with an engine 62 operable to generate electricity and/or steam. Engine 62 may be associated with reactor 64. In some embodiments, gasifier 52 may include container 54 operable for receiving biomass, dryer 56 operable for drying the biomass, pyrolysis chamber 58 operable for pyrolyzing the biomass into biochar, and container 60 operable for receiving the formed biochar. [0089] In some embodiments, the methods of the present disclosure may utilize the systems of the present disclosure to form the compositions of the present disclosure. For instance, with reference to system 50 in FIG.1D and the flow chart outlined in FIG.1E, the methods of the present disclosure include a step of forming biochar by placing biomass in a gasifier 52, where gasifier 52 is associated with an engine 62 operable to generate electricity and/or steam (step 30 in FIG. 1E). In some embodiments, biomass may be placed in gasifier 52 through container 54. Thereafter, gasifier 52 produces biochar and syngas (step 32 in FIG.1E). Next, engine 62 generates electricity and/or steam from the produced syngas (step 34 in FIG.1E). Thereafter, the generated electricity and/or steam is utilized to alter basalt through the electricity and/or steam generated from engine 62 (step 36 in FIG. 1E). Finally, the altered basalt is mixed with the produced biochar (step 38 in FIG.1E) to form the composition of the present disclosure (step 40 in FIG.1E). [0090] The gasifiers of the present disclosure may produce biochar in various manners. For instance, in some embodiments illustrated in FIG.1D, the gasifier 52 may produce biochar through pyrolysis, such as in pyrolysis chamber 58. [0091] Electricity and/or steam generated from an engine may be utilized to alter basalts in various manners. For instance, in some embodiments illustrated in FIG. 1D, electricity and/or steam generated from engine 62 may be utilized to grind basalt into a powder form. Thereafter, the ground basalt may be placed in reactor 64 for further alteration.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0092] In some embodiments, the electricity and/or steam generated from engine 62 may be utilized to heat the basalt in reactor 64. In some embodiments, the engines of the present disclosure (e.g., engine 62) may generate steam. In some embodiments, steam generated from an engine may be utilized to alter the basalt. For instance, in some embodiments illustrated in FIG.1D, steam generated from engine 62 may be utilized to heat the basalt in reactor 64 to form altered basalt. In some embodiments, the heating occurs at a temperature of at least 100 °C. In some embodiments, the heating occurs under acidic conditions. [0093] In some embodiments, the engines of the present disclosure generate electricity. In some embodiments, the generated electricity from the engine powers the altering of the basalt. [0094] In some embodiments, the methods of the present disclosure may also be utilized to capture CO2 from an environment during the production of the composition. For instance, in some embodiments, basalt alteration releases positively charged ions in solution, thereby making the solution alkaline. The solution then absorb CO2 from air and convert the CO2 to bicarbonate, thereby contributing to CO2 capture. [0095] Applications and Advantages [0096] The methods and compositions of the present disclosure can provide numerous advantages. For instance, in some embodiments, the methods of forming the compositions of the present disclosure require the utilization of less starting materials. In some embodiments, the compositions of the present disclosure may require about 100 times less basalt than that to use in enhanced silicate rock weathering. Moreover, in many preferred embodiments, the compositions of the present disclosure do not contain harmful organic pollutants that are present in biochar. Moreover, the compositions of the present disclosure can include numerous nutrients. [0097] As such, the methods and compositions of the present disclosure can have various applications. For instance, in some embodiments, the compositions of the present disclosure may be deployed on a large scale (e.g., globally) to capture CO2 from various environments, such as croplands. Moreover, in some embodiments, the methods and compositions of the present disclosure can be utilized to simultaneously enhance the nutrient content of the environment during the capture of CO2.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0098] In some preferred embodiments, the methods and compositions of the present disclosure can be utilized to simultaneously reduce atmospheric CO2 and increase cropland soil fertility by (a) sequestering mineral bound refractory carbon in the soil, and (b) producing soluble bicarbonate ion (HCO3-) that has a mean residence time of 10,000 years in the ocean. In some embodiments, large- scale deployment of the compositions of the present disclosure material on cropland around the globe could result in removing billions of tons of atmospheric CO2 per year while improving soil fertility, decreasing soil acidity, increasing soil carbon, and increasing soil water content. [0099] Additional embodiments [00100] Reference will now be made to more specific embodiments of the present disclosure and experimental results that provide support for such embodiments. However, Applicant notes that the disclosure below is for illustrative purposes only and is not intended to limit the scope of the claimed subject matter in any way. [00101] Example 1. Alteration of basalt [00102] The kinetics of weathering of basalt is extremely slow (Strefler et al., 2018). For instance, the overall dissolution rate for basalt crushed to 20 µm is ~3 x 10-11 mol m2 s-1 at a pH of 7. The weathering rate increases at low pH and at high temperature. For basalt glass that is hydrothermally altered at 200 ˚C in 100 mM acetic acid (pH = 4.63), the dissolution rate is about ~5 x 10-8 mol m2 s-1 (Peretyazhko et al., 2016) or about 1000-times faster than at room temperature. This example uses crystalline Mt. Holyoke Basalt (diameter = 600-1000 µm; BET surface area = 1.57 m2 g-1) to evaluate dissolution rates in terms of release of Ca2+, Mg2+, Na+, K+ ions with de-ionized water, 100 mM acetic acid, 100 mM citric acid, 100 mM pyroligneous acid (wood vinegar, ~50% acetic acid), and 100 mM HNO3 at 200 ˚C (Table 1). This example shows in that comparison to nitric acid, citric acid and especially the acetic is highly effective in partially altering the basalt and releasing alkali and alkaline earths. Table 1. Log of release rates (in mol m2 s-1) of Ca2+, Mg2+, Na+, K+ ions from Mt. Holyoke Basalt.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 Ca Ca Mg Mg Na Na K K Expt-1 Expt-2 Expt-1 Expt-2 Expt-1 Expt-2 Expt-1 Expt-2 DI water -10.59 -10.44 -11.21 -11.45 -10.89 -10.21 -11.21 -11.45 acetic -8.87 -8.92 -10.76 -10.85 -9.74 -9.96 -10.76 -10.85 citric -9.06 -9.12 -11.02 -11.01 -9.94 -10.26 -11.02 -11.01 pyroligneous -10.00 -10.06 -10.98 -11.24 -9.86 -10.12 -10.98 -11.24 HNO3 -8.83 -8.86 -11.19 -10.91 -9.82 -9.87 -11.19 -10.91 [00103] Example 2. Use of Fortified Biochar to Remove CO2 and Improve Soil Fertility [00104] This Example seeks to evaluate the potential of a novel nutrient-and carbon- rich soil amendment to sequester atmospheric CO2. In particular, Applicant has synthesized a novel soil amendment that is an organo-mineral composite, constituting biochar that is fortified with altered basalt (ABFB), whose application to soils sequesters atmospheric CO2. Additionally, this amendment is expected to improve soil fertility by providing nutrients to soils, decreasing soil acidity, increasing soil carbon, and increasing soil water content. [00105] Example 2.1. ABFB synthesis [00106] Applicant synthesized ABFB by reacting basalt powder with 100 mM acetic acid in an anoxic chamber at 200 °C for 24 h and then by mixing the resulting slurry with biochar prepared by pyrolysis of pine needles at 650 °C. Without being bound by theory, ABFB preparation is based on the following concepts: (a) energy and wood vinegar (~50% acetic acid) generated during pyrolysis of biomass to create biochar can be used to accelerate basalt weathering rate; (b) alteration of basalt with dilute acetic acid produces secondary clay minerals (Fe/Mg smectite) (Peretyazhko et al., 2016) and releases plant nutrients (Ca, Mg, K, P, S, Fe, Cu, Zn, Mn); (c) mixing altered basalt with biochar increases pH (~7.5), thereby promoting iron-oxyhydroxides precipitation, allowing sorption of organics on clay minerals; (d) heating of the mixture combined with iron-oxyhydroxides precipitation causes degradation of polycyclic aromatic hydrocarbon (PAHs) (Jia et al., 2014, Kołtowski and Oleszczuk, 2015), and (e) nutrients released from altered basalt fortify the biochar, which itself is a source of N as well as K and P that also come from basalt alteration. The ABFB is thus a novel soil amendment constituting organo-clay and organo-Fe-oxyhydroxide complexes whose application to soils would engender CO2 removal (CDR) and improve productivity.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00107] Example 2.2. Amendment of soil with ABFB [00108] Without being bound by theory, Applicant envisions that amendment of soil with ABFB can lead to proliferation of bacteria and arbuscular mycorrhizal fungi (Warnock et al., 2007) and accumulation of additional carbon in less decomposable fungal biomass. Second, at a slightly alkaline pH, both smectite and biochar will have a negative surface charge, allowing sorption of cations and some organic moieties. Additionally, these systems will be close to the point of zero charge of iron-oxyhydroxides and promote retention of negatively charged organic moieties and nutrients (e.g., phosphate) (Joseph et al., 2018, Shepherd et al., 2017b). Finally, ABFB would also engender CDR directly through highly refractory carbon in biochar and through the formation of bicarbonate ions. Soil amendments with ABFB would thus lead to a multipronged carbon sequestration: (a) in the soil—sequestration of highly aromatic refractory carbon, carbon adsorbed by iron-oxyhydroxides, carbon occluded by clay-minerals; and (b) in groundwater—release as dissolved bicarbonate ion which could eventually be transported to the ocean where its mean residence time is about 10,000 years. [00109] As illustrated in FIGS. 2A-2B, Applicant demonstrated that ABFB enhanced soil fertility for growing moong beans. FIG.2A shows different samples of three weeks old moong beans in amended Windsor Loam soil of the Connecticut River Valley collected from the Dartmouth Organic Farm. The control soil contains 0.9% Carbon and has a pH of 6.07. The soil was air-dried, sieved, and homogenized. Thereafter, the soil was amended with basalt, hydrothermally altered basalt, ABFB, and biochar. It was then packed on Biorad columns as shown. [00110] The ABFB and biochar amendments increased the carbon content of the soil to 3.62% and 4.93%, respectively. The total mass of soil (plus amendments) in each column was 180 g. Moong beans sprouted in de-ionized water were planted in each of the columns. Precise volumes of de-ionized water were passed through the columns and effluents collected and analyzed for nutrients, major, and trace metals. The plants grew in artificial light (9:15 :: light:dark cycle). [00111] FIG.2B shows the roots of the plants in FIG.2A. The images demonstrate that Moong bean plants grown with ABFB had the best developed roots, the longer trunks, and the larger leaves.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00112] Table 2 provides the calculated C and N concentrations in amended soils in FIG.2A. The table then summarizes the molar ratio of the nutrients (K, N, P) released in effluent over those released by control soil, effluent pH and alkalinity from each of the amended soils. As indicated in Table 2, the soil containing ABFB column releases the highest alkalinity. The median pH of the effluent from the ABFB column (= 7.67) indicates that the bulk of the alkalinity is in the form of bicarbonate ion. The ABFB amended soil released the highest amounts of K and P compared to those amended with basalt, altered basalt, or biochar. The ABFB amended soil also retained its N in comparison to soil with other amendments. These effluent characteristics are the possible reasons for increased soil fertility of ABFB amended soil compared to others. Table 2. Carbon and nitrogen contents of amended soil, release of K, N, and P from soil, its pH and estimated Alkalinity (in equivalent L-1). C N K N P pH Alkalinity (wt%) (wt%) Basalt + Soil 0.87 0.07 3.1 33.3 0.78 7.46 6 Altered basalt 0.7 1.17 6 + Soil 0.87 0.07 1.32 7.30 ABFB + Soil 3.62 0.11 239 0.49 2.15 7.67 26 Biochar + Soil 4.93 0.13 75 0.96 1.88 8.17 16 [00113] Example 2.3. Discussion [00114] In sum, hydrothermal alteration of basalt using low molecular weight organic acids (such as pyroligneous, acetic, citric, and oxalic acids) can accelerate basalt weathering rate by 100- to 1000-fold. This process alters basalts into secondary clay minerals and releases plant nutrients (Ca, Mg, K, P, S, Fe, Cu, Zn, Mn). Mixing altered basalt with biochar allows sorption of organic on clay minerals. Additionally, mixing of alkaline biochar promotes solution pH shifts to >7 allowing precipitation of iron-oxyhydroxides that further trap organics.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00115] Nutrients released from altered basalt fortify the biochar, which itself is a source of K, N, and P. The resulting slurry of altered basalt with fortified biochar (ABFB) is a novel soil amendment constituting an organo-clay composite whose application to soils would sequester atmospheric CO2 both on land and in the ocean. In Applicant’s experiments, for 10 g of ABFB added to soil, about 5 g carbon would be sequestered in soil and 0.32 g carbon would be sequestered as bicarbonate in the ocean. Thus, it is expected that about 0.5 tons of CO2 would be removed per ton of ABFB applied per year. [00116] Additionally, application of ABFB is expected to improve soil fertility by providing nutrients to soils, decreasing soil acidity, increasing soil carbon, and increasing water content. Applicant’s experiments also show that ABFB is a better solution than just basalt, altered basalt, or biochar in improving soil fertility. As such, ABFB has the potential to be deployed in the field and on a large scale to remove atmospheric CO2. [00117] Example 3. Production of ABFB [00118] This Example provides various processes for generating ABFB. For instance, FIG.3 illustrates the production of ABFB using electricity generated from syngas, where the syngas is produced by a biochar producing gasifier (i.e., an All Power Labs PP30 Power Pallet gasifier). Biomass (e.g., wood shavings) is first placed in a gasifier to generate biochar through pyrolysis at ≥ 650 ˚C. Syngas produced as a byproduct is utilized to generate electricity. [00119] The electricity generated from the engine is then used to grind basalt into a powder form and sieve it to obtain the adequate size. The ground basalt is then placed in a reactor with dilute acetic/citric acid (i.e., a Buechiglas kiloclave® lab pressure reactor). The reactor is powered by the electricity generated during biochar production, also using the steam produced due to the combustion of syngas. The basalt is hydrothermally altered in the reactor at around 200 °C. Finally, the altered basalt is mixed with the produced biochar in the reactor and heated to 120 °C using electricity and hot water from gasifier to form ABFB (i.e., fortified biochar in a slurry)| [0003] PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00120] FIG. 4 illustrates another ABFB production process that can be streamlined by deploying two reactors (i.e., two Buechiglas kiloclave® lab pressure reactors). The electricity generated from the engine attached to a gasifier (i.e., an All Power Labs PP30 Power Pallet gasifier) is used to grind basalt into a powder form and sieve it to obtain the adequate size. The ground basalt is then placed in Reactor-1 with dilute acetic/citric acid. The reactor is powered by the electricity generated during biochar production, also using the steam produced due to the combustion of syngas. The basalt is hydrothermally altered in Reactor-1 at around 200 °C. The altered basalt is then mixed with the produced biochar in Reactor-2 and heated to 120 °C using electricity and steam from gasifier to form ABFB (i.e., fortified biochar in a slurry). [00121] Different gasifiers and reactors may be used to scale up ABFB production to take advantage of the economy of scale. The formed ABFB may then be processed in various manners. For instance, the ABFB may be dried for spreading on land through the utilization of existing equipment. It may also be pelletized, if needed. The ABFB may be spread as a slurry using existing equipment after modifying its consistency to use with slurry spreading equipment. [00122] FIG.5 illustrates another ABFB production process that involves the following steps. First, basalt is ground to about 20 µm. The powdered basalt is then mixed with wood vinegar in water and heated at 200 °C for 24 hours. Finally, biochar produced from pine needles at 650 °C is homogenized with the powdered and altered basalt at 120 °C and a pH of 7 to form ABFB. [00123] FIG.6 illustrates another ABFB production process that involves the following steps. First, basalt is ground to about 20 µm. In parallel, biochar is produced by heating at 450 °C in a self- heated oven with wood vinegar as the by-product. The powdered basalt is then mixed with wood vinegar in water and heated at 200 °C. In some embodiments, the biochar is heated in an oven at 650 °C and mixed with altered basalt and homogenized. In other embodiments, biochar produced by heating at 450 °C in a self-heated oven is added directly to the altered basalt and homogenized to form ABFB. [00124] FIG.7 illustrates another ABFB production process that involves using Deccan basalt from India. The basalt is initially ground to 200-800 µm. The powdered basalt is then mixed with wood vinegar in water and heated at 200 °C. Finally, commercial biochar produced at 450 °C in a self-heated oven is sieved to 200-800 µm and homogenized with the powdered and altered basalt at 120 °C and a pH of 7.5 to form ABFB.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00125] FIG. 8 shows an image of an ABFB formed in accordance with the methods of the present disclosure. [00126] References [00127] AMONETTE, J. E., BLANCO-CANQUI, H., HASSEBROOK, C., LAIRD, D. A., LAL, R., LEHMANN, J. & PAGE-DUMROESE, D.2021. Integrated biochar research: A roadmap. Journal of Soil and Water Conservation, 76, 24A-29A. [00128] BEERLING, D. J., EPIHOV, D. Z., KANTOLA, I. B., MASTERS, M. D., REERSHEMIUS, T., PLANAVSKY, N. J., REINHARD, C. T., JORDAN, J. S., THORNE, S. J. & WEBER, J.2024. Enhanced weathering in the US Corn Belt delivers carbon removal with agronomic benefits. 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Effects of mineralogy, chemistry and physical properties of basalts on carbon capture potential and plant-nutrient element release via enhanced weathering. Applied Geochemistry, 132, 105023. [00147] MAŠEK, O., BUSS, W., BROWNSORT, P., ROVERE, M., TAGLIAFERRO, A., ZHAO, L., CAO, X. & XU, G.2019. Potassium doping increases biochar carbon sequestration potential by 45%, facilitating decoupling of carbon sequestration from soil improvement. Scientific reports, 9, 5514. [00148] ODINGA, E. S., GUDDA, F. O., WAIGI, M. G., WANG, J. & GAO, Y.2021. Occurrence, formation and environmental fate of polycyclic aromatic hydrocarbons in biochars. Fundamental Research, 1, 296-305. [00149] PERETYAZHKO, T. S., SUTTER, B., MORRIS, R. V., AGRESTI, D. G., LE, L. & MING, D. W.2016. Fe/Mg smectite formation under acidic conditions on early Mars. Geochimica Et Cosmochimica Acta, 173, 37-49. [00150] RAWAL, A., JOSEPH, S. D., HOOK, J. M., CHIA, C. H., MUNROE, P. R., DONNE, S., LIN, Y., PHELAN, D., MITCHELL, D. R. G., PACE, B., HORVAT, J. & WEBBER, J. B. W.2016. Mineral-Biochar Composites: Molecular Structure and Porosity. Environmental Science & Technology, 50, 7706-7714. [00151] RODRIGUEZ FRANCO, C., PAGE-DUMROESE, D. S., PIERSON, D. & NICOSIA, T.2024. Biochar Utilization as a Forestry Climate-Smart Tool. Sustainability, 16, 1714. [00152] ROMBOLÀ, A. G., FABBRI, D., BARONTI, S., VACCARI, F. P., GENESIO, L. & MIGLIETTA, F.2019. Changes in the pattern of polycyclic aromatic hydrocarbons in soil treated with biochar from a multiyear field experiment. Chemosphere, 219, 662-670. [00153] SCHMIDT, M. W. I., TORN, M. S., ABIVEN, S., DITTMAR, T., GUGGENBERGER, G., JANSSENS, I. A., KLEBER, M., KOGEL-KNABNER, I., LEHMANN, J., MANNING, D. A. C., NANNIPIERI, P., RASSE, D. P., WEINER, S. & TRUMBORE, S. E.2011. Persistence of soil organic matter as an ecosystem property. Nature, 478, 49-56. [00154] SCHUILING, R. & KRIJGSMAN, P.2006. Enhanced weathering: an effective and cheap tool to sequester CO2. Climatic Change, 74, 349-354.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00155] SHEPHERD, J. G., BUSS, W., SOHI, S. P. & HEAL, K. V.2017a. Bioavailability of phosphorus, other nutrients and potentially toxic elements from marginal biomass-derived biochar assessed in barley (Hordeum vulgare) growth experiments. Science of the Total Environment, 584, 448-457. [00156] SHEPHERD, J. G., JOSEPH, S., SOHI, S. P. & HEAL, K. V.2017b. Biochar and enhanced phosphate capture: Mapping mechanisms to functional properties. Chemosphere, 179, 57- 74. [00157] SHRESTHA, R. K., JACINTHE, P. A., LAL, R., LORENZ, K., SINGH, M. P., DEMYAN, S. M., REN, W. & LINDSEY, L. E.2023. Biochar as a negative emission technology: A synthesis of field research on greenhouse gas emissions. Journal of Environmental Quality, 52, 769- 798. [00158] STREFLER, J., AMANN, T., BAUER, N., KRIEGLER, E. & HARTMANN, J. 2018. Potential and costs of carbon dioxide removal by enhanced weathering of rocks. Environmental Research Letters, 13. [00159] TAYLOR, L. L., QUIRK, J., THORLEY, R., KHARECHA, P. A., HANSEN, J., RIDGWELL, A., LOMAS, M. R., BANWART, S. A. & BEERLING, D. J.2016. Enhanced weathering strategies for stabilizing climate and averting ocean acidification. Nature Climate Change, 6, 402-406. [00160] WARNOCK, D. D., LEHMANN, J., KUYPER, T. W. & RILLIG, M. C.2007. Mycorrhizal responses to biochar in soil–concepts and mechanisms. Plant and soil, 300, 9-20. [00161] WILSON, M.1989. Igneous petrogenesis, Springer. [00162] WINTER, J. D.2014. Principles of igneous and metamorphic petrology, Pearson education Harlow, UK. [00163] WOOLF, D., AMONETTE, J. E., STREET-PERROTT, F. A., LEHMANN, J. & JOSEPH, S.2010. Sustainable biochar to mitigate global climate change. Nature Communications, 1. [00164] XIA, L., CAO, L., YANG, Y., TI, C., LIU, Y., SMITH, P., VAN GROENIGEN, K. J., LEHMANN, J., LAL, R. & BUTTERBACH-BAHL, K.2023. Integrated biochar solutions can achieve carbon-neutral staple crop production. Nature Food, 4, 236-246.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00165] XIAO, X., CHEN, B., CHEN, Z., ZHU, L. & SCHNOOR, J. L.2018. Insight into multiple and multilevel structures of biochars and their potential environmental applications: a critical review. Environmental science & technology, 52, 5027-5047. [00166] YANG, Y., SUN, K., HAN, L. F., JIN, J., SUN, H. R., YANG, Y. & XING, B. S.2018. Effect of minerals on the stability of biochar. Chemosphere, 204, 310-317. [00167] Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the present disclosure to its fullest extent. The embodiments described herein are to be construed as illustrative and not as constraining the remainder of the disclosure in any way whatsoever. While the embodiments have been shown and described, many variations and modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. Accordingly, the scope of protection is not limited by the description set out above, but is only limited by the claims, including all equivalents of the subject matter of the claims. The disclosures of all patents, patent applications and publications cited herein are hereby incorporated herein by reference, to the extent that they provide procedural or other details consistent with and supplementary to those set forth herein. (WO2024/220896)|[0001] PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-03 TITLE CARBON DIOXIDE REMOVAL WITH BIOCHAR FORTIFIED BY ACCELERATED WEATHERING OF BASALT (ABFB) CROSS-REFERENCE TO RELATED APPLICATIONS [0001] This application claims priority to U.S. Provisional Patent Application No.63/460,553, filed on April 19, 2023; U.S. Provisional Patent Application No.63/599,946, filed on November 16, 2023; and U.S. Provisional Patent Application No.63/557,387, filed on February 23, 2024. The entirety of each of the aforementioned applications is incorporated herein by reference. BACKGROUND [0002] Current methods and compositions for capturing carbon dioxide from environments have numerous limitations. Embodiments of the present disclosure aim to address the aforementioned limitations. SUMMARY [0003] In some embodiments, the present disclosure pertains to a composition that includes at least one basalt and at least one biochar. In some embodiments, the biochar includes nutrient fortified biochar. In some embodiments, the nutrients are derived from the basalt. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof. [0004] In some embodiments, the basalt in the compositions of the present disclosure include altered basalt. In some embodiments, the altered basalt includes powdered basalt, heated basalt, or combinations thereof. [0005] Additional embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure. In some embodiments, the compositions of the present disclosure also enhance the nutrient content of the environment. For instance, in some embodiments where the environment includes soil, the compositions of the present disclosure also enhance the fertility of the soil. Additional embodiments of the present disclosure pertain to methods of enhancing soil fertility by applying a composition of the present disclosure to the soil.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0006] Further embodiments of the present disclosure pertain to methods of making a composition by altering at least one basalt and mixing the altered basalt with at least one biochar. In some embodiments, the altering occurs by heating the basalt under acidic conditions. In some embodiments, the altering includes grinding the basalt to form a powder. [0007] In some embodiments, the mixing of altered basalt with biochar results in nutrient fortification of the biochar by the nutrients derived from the altered basalt. In some embodiments, the methods of the present disclosure also include a step of forming the biochar. In some embodiments, biochar formation occurs by heating a biomass, such as through pyrolysis. In some embodiments, the methods of the present disclosure may also be utilized to prevent the release of carbon dioxide (CO2) from the biomass during biochar production. [0008] In some embodiments, the methods of the present disclosure occur through the following steps: (1) forming the biochar, where the forming includes placing a biomass in a gasifier associated with an engine operable to generate electricity and/or steam, where the gasifier produces biochar and syngas, and where the engine generates electricity and/or steam from the syngas; (2) altering the basalt by utilizing the electricity and/or steam generated from the engine; and (3) mixing the altered basalt with the produced biochar to form the composition. In some embodiments, the engines of the present disclosure may generate steam (e.g., hot water). In some embodiments, the steam (e.g., hot water) generated from an engine may be utilized to alter the basalt. In some embodiments, the engines of the present disclosure may generate electricity. In some embodiments, the electricity generated from the engine may be utilized to alter the basalt. DRAWINGS [0009] FIG. 1A illustrates a method capturing carbon dioxide (CO2) from an environment in accordance with various embodiments of the present disclosure. [0010] FIG.1B illustrates a method of enhancing soil fertility in a subject in accordance with various embodiments of the present disclosure. [0011] FIG. 1C illustrates a method of making a basalt-biochar composition in accordance with various embodiments of the present disclosure.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0012] FIG. 1D provides a diagram of a system for making a basalt-biochar composition in accordance with various embodiments of the present disclosure. [0013] FIG. 1E illustrates an alternative method of making a basalt-biochar composition in accordance with various embodiments of the present disclosure. [0014] FIGS.2A-2B provide experimental results demonstrating that the basalt-biochar compositions of the present disclosure enhance soil fertility. [0015] FIGS.3-4 illustrate schemes for the production of altered basalt with fortified biochar (ABFB) using electricity generated from syngas, where the syngas is produced by a biochar producing gasifier. [0016] FIGS. 5-7 illustrate additional processes of forming ABFB in accordance with various embodiments of the present disclosure. [0017] FIG. 8 shows an image of an ABFB formed in accordance with the methods of the present disclosure. DETAILED DESCRIPTION [0018] It is to be understood that both the foregoing general description and the following detailed description are illustrative and explanatory, and are not restrictive of the subject matter, as claimed. In this application, the use of the singular includes the plural, the word “a” or “an” means “at least one”, and the use of “or” means “and/or”, unless specifically stated otherwise. Furthermore, the use of the term “including”, as well as other forms, such as “includes” and “included”, is not limiting. Also, terms such as “element” or “component” encompass both elements or components comprising one unit and elements or components that include more than one unit unless specifically stated otherwise. [0019] The section headings used herein are for organizational purposes and are not to be construed as limiting the subject matter described. All documents, or portions of documents, cited in this application, including, but not limited to, patents, patent applications, articles, books, and treatises, are hereby expressly incorporated herein by reference in their entirety for any purpose. In the event that one or more of the incorporated literature and similar materials defines a term in a manner that contradicts the definition of that term in this application, this application controls.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0020] Carbon dioxide (CO2) removal (CDR) is a key process for addressing climate change. There are two prominent CDR strategies for addressing climate change: enhanced silicate rock weathering (EW) (Beerling et al., 2024, Beerling et al., 2020, Beerling et al., 2018, Taylor et al., 2016, Lewis et al., 2021, Schuiling and Krijgsman, 2006) and application of biochar (Kambo and Dutta, 2015, Lehmann et al., 2015, Lehmann et al., 2021, Rodriguez Franco et al., 2024, Woolf et al., 2010, Xia et al., 2023, Xiao et al., 2018, Amonette et al., 2021, Lehmann, 2007, Schmidt et al., 2011). However, both strategies have significant drawbacks. [0021] In particular, the EW strategy involves crushing basalt to a fine powder to speed-up weathering reactions. This strategy, however, still suffers from slow reaction kinetics (Strefler et al., 2018). For instance, to remove 1 Pg C per year would require about 21 Pg of basalt to be mined, ground to 20 μm, and spread on croplands every year. [0022] Use of biochar is yet another strategy for CDR (Lehmann et al., 2021, Shrestha et al., 2023). Preparation of biochar involves heating biomass (e.g., wood and/or crop residues) in an airless oven at temperatures ranging from 300 °C to 800 °C. Biochar carbon should be stable in soil for over centuries to be of value for long-term CDR (Lehmann et al., 2015). In fact, it has been shown that biochar prepared at 600 °C or higher is especially recalcitrant (Lehmann et al., 2021). Oxidative resistance and occlusion by clay minerals may combine to make biochar (Mašek et al., 2019, Rawal et al., 2016, Yang et al., 2018) persist in soil for hundreds of years. [0023] Adapting biochar globally as a soil amendment can affect both CDR and greenhouse gas emissions (Lehmann et al., 2021). However, several studies have shown that organic pollutants (e.g., polycyclic aromatic hydrocarbons (PAHs)) are synthesized during biochar preparation (Godlewska et al., 2021, Hale et al., 2012, Kołtowski and Oleszczuk, 2015, Odinga et al., 2021). These pollutants can remain in the soil, making its application to croplands questionable (Rombolà et al., 2019, Shepherd et al., 2017a). [0024] Furthermore, preparation of biochar also releases roughly similar amounts of liquid and gaseous CO2 (CO2e) thereby reducing CDR efficiency by a factor of about 1.9. In particular, for every ton of biochar produced, about 0.74 ton of CO2e (gases and liquids) is released (Crombie and Mašek, 2015).PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0025] As such, a need exists for more effective and less hazardous materials for CDR. A need also exists for safer and more effective methods of mass producing such materials. Numerous embodiments of the present disclosure aim to address the aforementioned needs. [0026] Compositions [0027] In some embodiments, the present disclosure pertains to a composition. In some embodiments, the composition includes at least one biochar and at least one basalt. In some embodiments, the biochar and basalt are associated with one another. As set forth in more detail herein, the compositions of the present disclosure can include various basalts and biochars in various arrangements. [0028] Biochar [0029] Biochar generally refers to a condensed aromatic carbon rich substance that forms when biomass (e.g., wood and/or crop residues) is heated in a container at a high temperature (e.g., temperatures ranging from 300 °C to 800 °C with little or no available oxygen (i.e., pyrolysis)). The compositions of the present disclosure can include various types of biochar. For instance, in some embodiments, the biochar includes alkaline biochar. In some embodiments, the biochar includes corn husk biochar. In some embodiments, the biochar includes nutrient fortified biochar. In some embodiments, the nutrients are derived from the basalt. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof. [0030] Basalts [0031] Basalt generally refers to a mafic aphanitic volcanic rock that includes, without limitation, tholeiites (Best, 2013, Cox et al., 1979, Hughes, 2013, Wilson, 1989, Winter, 2014, Carmichael et al., 1974). Basalt is exposed around the world on the continents and at the ocean floor. [0032] The composition of the present disclosure can also include various types of basalts. For instance, in some embodiments, the basalts include, without limitation, plagioclase feldspars- containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. In some embodiments, the basalts contain, without limitation, plagioclase feldspars-pyroxenes, with or without any olivine.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0033] In some embodiments, basalts in the compositions of the present disclosure include plagioclase feldspars-containing basalts and pyroxenes-containing basalts. In some embodiments, basalts in the compositions of the present disclosure include microscopic or visible plagioclase feldspars-containing basalts and pyroxenes-containing basalts, with little or no olivines, and with minor iron spinel and phosphate. [0034] The basalts in the compositions of the present disclosure could be from several basalt regions around the world and/or from various localities. For instance, in some embodiments, the basalts in the compositions of the present disclosure may include Holyoke Basalt (MA) and Butner Basalt (NC), which belong to Central Atlantic Magmatic Province that is exposed along the US Eastern Seaboard, Columbia River Flood Basalt, Deccan Traps, Karoo Basalts, Parana Basalts, Siberian Traps, Hawaiian Basalts, Icelandic Basalts, or other regions. [0035] In some embodiments, the basalts in the compositions of the present disclosure include tholeiites. In some embodiments, the basalts in the compositions of the present disclosure include tholeiites with low heavy metal concentrations. [0036] In some embodiments, the basalts in the compositions of the present disclosure include Holyoke Basalt. In some embodiments, the basalts in the compositions of the present disclosure include Deccan Basalt. [0037] In some embodiments, the basalts in the compositions of the present disclosure have been naturally altered. In some embodiments, the basalts in the compositions of the present disclosure are in isolated form (i.e., basalt isolated from its native environment, such as through mining). In some embodiments, the basalts in the compositions of the present disclosure include mined basalt. In some embodiments, the basalts in the compositions of the present disclosure include basalt that have been crushed and ground to a range of grain-sizes. In some embodiments, the basalts in the compositions of the present disclosure include basalt that have been partially altered to clay minerals.| [0002] PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0038] In some embodiments, the basalts in the basalts in the compositions of the present disclosure include altered basalt. In some embodiments, the altered basalt is in powdered form. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 1 mm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 800 µm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 500 µm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 100 µm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 50 µm. In some embodiments, the powdered basalt has diameters ranging from about 10 µm to about 20 µm. [0039] In some embodiments, the powdered basalt may be in the form of particles. In some embodiments, the powdered basalt particles may be in the form of coarse particles, medium particles, coarse-grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. [0040] In some embodiments, the altered basalt includes heated basalt. In some embodiments, the heated basalt is heated at a temperature of at least 100 °C. In some embodiments, the heated basalt is heated at a temperature of at least 150 °C. In some embodiments, the heated basalt is heated at a temperature of at least 200 °C. In some embodiments, the heated basalt is heated under acidic conditions. [0041] Composition forms [0042] The compositions of the present disclosure may be in various forms. For instance, in some embodiments, the compositions of the present disclosure include altered basalt. In some embodiments, the compositions of the present disclosure include biochar that has been fortified with nutrients from altered basalt (ABFB). In some embodiments, the nutrients are derived from altered basalt. In some embodiments, the nutrients are derived from altered basalt and from biochar. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, N, salts thereof, oxides thereof, or combinations thereof.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0043] The ABFBs of the present disclosure can include various ratios of biochar and altered basalt. For instance, in some embodiments, the biochar: altered basalt ratio could vary from 0 to 0.25. In some embodiments, the biochar: altered basalt ratio could vary from 0 to 0.5. In some embodiments, the biochar: altered basalt ratio could vary from 0 to 0.75. In some embodiments, the biochar: altered basalt ratio could vary from 0 to 1.0. In some embodiments, the biochar: altered basalt ratio is about 0.25. In some embodiments, the biochar: altered basalt ratio is about 0.5. In some embodiments, the biochar: altered basalt ratio is about 0.75. In some embodiments, the biochar: altered basalt ratio is about 1. [0044] In some embodiments, the compositions of the present disclosure are in the form of a slurry. In some embodiments, the compositions of the present disclosure are in homogenized form. In some embodiments, the compositions of the present disclosure include organo-clay complexes, organo-Fe- oxyhydroxide complexes, or combinations thereof. [0045] Methods of capturing carbon dioxide (CO2) from an environment [0046] Additional embodiments of the present disclosure pertain to a method of capturing carbon dioxide (CO2) from an environment. In some embodiments illustrated in FIG.1A, the methods of the present disclosure include exposing the environment to a composition of the present disclosure (step 10) to result in the capture of the CO2 form the environment (step 12). In some embodiments, the compositions of the present disclosure also enhance the nutrient content of the environment (step 14). As set forth in more detail herein, the methods of the present disclosure can be utilized to capture various types of CO2 from various environments. [0047] Carbon dioxide (CO2) [0048] The method of the present disclosure may be utilized to capture various types of CO2. For instance, in some embodiments, the CO2 to be captured include, without limitation, carbon dioxide CO2 from air, soil and/or water. [0049] Without being bound by theory, the capture of CO2 by the compositions of the present disclosure can occur through various mechanisms. For instance, in some embodiments, the capturing of the CO2 occurs by a method that includes, without limitation, dissolution, pyrolysis, adhesion, binding, adsorption, electrostatic interaction, or combinations thereof. [0050] Exposure of environment to a compositionPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0051] The methods of the present disclosure may be utilized to capture CO2 from various environments. For instance, in some embodiments, the environment includes, without limitation, an airstream, a gas stream, an industrial plant, an atmosphere, ambient air, a water source, soil, or combinations thereof. In some embodiments, the environment includes ambient air. In some embodiments, the environment includes an atmosphere. [0052] In some embodiments, the environment includes a water source. In some embodiments, the water source includes, without limitation, a body of water, an ocean, a sea, a lake, a pond, or combinations thereof. In some embodiments, the water source includes a sea. In some embodiments, the water source includes an ocean. [0053] In some embodiments, the environment includes soil. In some embodiments, the soil is part of a field. In some embodiments, the field includes, without limitation, an agricultural field, a residential field, a cropland, a park, a subdivision, a yard, a highway, a sports facility, a golf course, or combinations thereof. [0054] The compositions of the present disclosure may be exposed to an environment in various manners. For instance, in some embodiments, the exposing occurs by flowing the environment through the composition. In some embodiments, the exposing occurs by placing the composition at or near the environment. [0055] In some embodiments, the exposing of an environment to a composition of the present disclosure occurs by a method that includes, without limitation, incubating, spreading, pouring, sprinkling, spraying, or combinations thereof. In some embodiments where the environment includes soil, the compositions of the present disclosure may be exposed to the soil by sprinkling the composition onto the soil. [0056] Desirable levels of soil organic carbon below which crop yield declines may be ~2% in soils of the temperate zone and ~1% for those of the tropics (Lal, 2020). Soils with organic carbon contents exceeding 5% are highly fertile (Lal, 2020). In some embodiments, the compositions of the present disclosure (e.g., ABFBs) can be used to boost soil organic carbon content. Depending on their compositions, the compositions of the present disclosure (e.g., ABFBs) can be deployed on cropland and degraded soils such that they reach or exceed a desirable level in a single application of ABFB. [0057] Enhancement of nutrient content of environmentPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0058] In some embodiments, the compositions of the present disclosure also enhance the nutrient content of the environment. For instance, in some embodiments, exposure of the compositions of the present disclosure to an environment result in the enhancement of Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, and/or N in the environment. [0059] The enhancement of the nutrient content of environments can have various advantageous effects. For instance, in some embodiments where the environment includes soil, the compositions of the present disclosure may enhance soil fertility. [0060] Methods of enhancing soil fertility [0061] Additional embodiments of the present disclosure pertain to a method of enhancing soil fertility. In some embodiments illustrated in FIG.1B, the methods of the present disclosure include exposing the soil to a composition of the present disclosure (step 16) to result in the enhancement of the soil’s fertility (step 18). [0062] Exposure of soil to a composition [0063] The compositions of the present disclosure may be exposed to soil in various manners. For instance, in some embodiments, the exposing of a soil to a composition of the present disclosure occurs by a method that includes, without limitation, incubating, spreading, pouring, sprinkling, spraying, or combinations thereof. In some embodiments, exposing of a soil to a composition of the present disclosure occurs by sprinkling the composition onto the soil. In some embodiments, exposing of a soil to a composition of the present disclosure occurs by spraying the composition onto the soil. [0064] Soils [0065] The compositions of the present disclosure may be applied to various types of soils. For instance, in some embodiments, the soil is part of a field. In some embodiments, the field includes, without limitation, an agricultural field, a residential field, a cropland, a park, a subdivision, a yard, a highway, a sports facility, a golf course, or combinations thereof. [0066] Enhancement of soil fertilityPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0067] Without being bound by theory, the compositions of the present disclosure may enhance a soil’s fertility in various manners. For instance, in some embodiments, the compositions of the present disclosure enhance soil fertility by at least providing nutrients to the soil, decreasing soil acidity, increasing soil carbon content, increasing soil water content, or combinations thereof. In some embodiments, the compositions of the present disclosure enhance soil fertility by at least providing nutrients to the soil. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, and/or N. [0068] The methods of the present disclosure may have various advantages. For instance, in some embodiments, the methods of the present disclosure may be utilized to enhance food security, reduce energy poverty, and address climate change. [0069] Methods of making compositions [0070] Additional embodiments pertain to a method of making the compositions of the present disclosure. In some embodiments, the method includes mixing at least one biochar with at least one basalt to form the compositions of the present disclosure. [0071] The methods of the present disclosure may be utilized to mix various types of basalts and biochars. Suitable basalts and biochars were described supra and are incorporated herein by reference. As set forth in more detail, the methods of the present disclosure can occur through various processes. [0072] Altering basalts [0073] In some embodiments, the methods of the present disclosure also include a step of altering a basalt. In some embodiments, the altering occurs prior to mixing the basalt with the biochar. [0074] Basalts may be altered through various processes. For instance, in some embodiments, altering includes grinding the basalt. In some embodiments, the altering results in the formation of a basalt powder. [0075] In some embodiments, the altering includes heating the basalt. In some embodiments, the heating occurs at a temperature of at least 100 °C. In some embodiments, the heating occurs at a temperature of at least 150 °C. In some embodiments, the heating occurs at a temperature of at least 200 °C.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0076] In some embodiments, basalts are heated under acidic conditions. For instance, in some embodiments, basalt may be heated in an acidic solution. In some embodiments, the acidic solution includes, without limitation, an acetic acid solution, a carbonic acid solution, a vinegar solution, a wood vinegar solution, a citric acid solution, an oxalic acid solution, a pyroligneous acid solution, or combinations thereof. In some embodiments, the heating occurs in an acidic solution at a temperature of at least 100 °C and a pH of less than 7. [0077] Forming biochar [0078] In some embodiments, the methods of the present disclosure also include a step of forming the biochar. Various methods may be utilized to form biochar. For instance, in some embodiments, biochar is formed by heating biomass. In some embodiments, the heating includes pyrolysis of the biomass. In some embodiments, heating occurs at a temperature of at least 300 °C. In some embodiments, the heating occurs at a temperature of at least 400 °C. In some embodiments, the heating occurs at a temperature of at least 500 °C. In some embodiments, the heating occurs at a temperature ranging from about 300 °C to about 800 °C. [0079] Biochars may be formed from various biomasses. For instance, in some embodiments, the biomass includes, without limitation, walnut shells, wood residues, hardwood chips, softwood chips, wood shavings, crop residues, or combinations thereof. [0080] In some embodiments, the methods of the present disclosure also involve preventing the emission of carbon dioxide (CO2) from biomass. It is widely understood that plants absorb CO2 during photosynthesis, transforming it into various organic compounds such as cellulose, hemicellulose, and/or lignin. Upon the plant's demise, this biomass undergoes remineralization, releasing CO2 back into the atmosphere. The creation of biochar from biomass has the potential to impede the process of remineralization, thereby preventing the conversion of carbon fixed during photosynthesis into CO2. [0081] Mixing of basalt and biocharPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0082] The methods of the present disclosure can utilize various processes to mix basalts and biochars. For instance, in some embodiments, the mixing includes homogenization. In some embodiments, the mixing occurs under alkaline conditions. In some embodiments, the mixing occurs at a pH of at least 7. In some embodiments, the mixing occurs at a pH of at least 7.5. [0083] In some embodiments, the mixing occurs above room temperature. For instance, in some embodiments, the mixing occurs at a temperature of 100 °C or higher. In some embodiments, the mixing occurs at a temperature of 120 °C or higher. In some embodiments, the mixing occurs at a temperature of 120 °C or higher. In some embodiments, the mixing occurs at a temperature of about 200 °C. [0084] In some embodiments, basalts may be mixed with biochars after being altered. For instance, in some embodiments illustrated in FIG. 1C, the methods of the present disclosure may include: altering the basalt (step 20) and mixing the altered basalt with biochar (step 22) to form a composition of the present disclosure (step 24). In some embodiments, the methods of the present disclosure also include a step of forming biochar (step 21) and then mixing the formed biochar with the altered basalt (step 22). [0085] Mixing biochars with basalts can have various effects. For instance, in some embodiments, the method results in nutrient fortification of the biochar. In some embodiments, the nutrients are derived from the basalt. In some embodiments, the nutrients include, without limitation, Ca, Mg, K, P, S, Fe, Cu, Zn, Mn, salts thereof, oxides thereof, or combinations thereof. In some embodiments, the method results in the association of one or more organic materials with the altered basalt. [0086] The methods of the present disclosure can be utilized to form various types of compositions. Suitable compositions were described supra and are incorporated herein by reference. For instance, in some embodiments, the formed composition has a pH of more than 7. In some embodiments, the alkaline pH provides a negative surface charge, thereby allowing sorption of various materials (e.g., cations and organic moieties) onto the altered basalt and biochar. In some embodiments, the formed composition includes organo-clay complexes, organo-Fe-oxyhydroxide complexes, or combinations thereof. [0087] Systems for the formation of compositionsPCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0088] The compositions of the present disclosure may be formed through the utilization of various systems. Additional embodiments of the present disclosure pertain to such systems for the formation of the compositions of the present disclosure. With reference to system 50 in FIG.1D for illustrative purposes, the systems of the present disclosure may include a gasifier 52 associated with an engine 62 operable to generate electricity and/or steam. Engine 62 may be associated with reactor 64. In some embodiments, gasifier 52 may include container 54 operable for receiving biomass, dryer 56 operable for drying the biomass, pyrolysis chamber 58 operable for pyrolyzing the biomass into biochar, and container 60 operable for receiving the formed biochar. [0089] In some embodiments, the methods of the present disclosure may utilize the systems of the present disclosure to form the compositions of the present disclosure. For instance, with reference to system 50 in FIG.1D and the flow chart outlined in FIG.1E, the methods of the present disclosure include a step of forming biochar by placing biomass in a gasifier 52, where gasifier 52 is associated with an engine 62 operable to generate electricity and/or steam (step 30 in FIG. 1E). In some embodiments, biomass may be placed in gasifier 52 through container 54. Thereafter, gasifier 52 produces biochar and syngas (step 32 in FIG.1E). Next, engine 62 generates electricity and/or steam from the produced syngas (step 34 in FIG.1E). Thereafter, the generated electricity and/or steam is utilized to alter basalt through the electricity and/or steam generated from engine 62 (step 36 in FIG. 1E). Finally, the altered basalt is mixed with the produced biochar (step 38 in FIG.1E) to form the composition of the present disclosure (step 40 in FIG.1E). [0090] The gasifiers of the present disclosure may produce biochar in various manners. For instance, in some embodiments illustrated in FIG.1D, the gasifier 52 may produce biochar through pyrolysis, such as in pyrolysis chamber 58. [0091] Electricity and/or steam generated from an engine may be utilized to alter basalts in various manners. For instance, in some embodiments illustrated in FIG. 1D, electricity and/or steam generated from engine 62 may be utilized to grind basalt into a powder form. Thereafter, the ground basalt may be placed in reactor 64 for further alteration.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0092] In some embodiments, the electricity and/or steam generated from engine 62 may be utilized to heat the basalt in reactor 64. In some embodiments, the engines of the present disclosure (e.g., engine 62) may generate steam. In some embodiments, steam generated from an engine may be utilized to alter the basalt. For instance, in some embodiments illustrated in FIG.1D, steam generated from engine 62 may be utilized to heat the basalt in reactor 64 to form altered basalt. In some embodiments, the heating occurs at a temperature of at least 100 °C. In some embodiments, the heating occurs under acidic conditions. [0093] In some embodiments, the engines of the present disclosure generate electricity. In some embodiments, the generated electricity from the engine powers the altering of the basalt. [0094] In some embodiments, the methods of the present disclosure may also be utilized to capture CO2 from an environment during the production of the composition. For instance, in some embodiments, basalt alteration releases positively charged ions in solution, thereby making the solution alkaline. The solution then absorb CO2 from air and convert the CO2 to bicarbonate, thereby contributing to CO2 capture. [0095] Applications and Advantages [0096] The methods and compositions of the present disclosure can provide numerous advantages. For instance, in some embodiments, the methods of forming the compositions of the present disclosure require the utilization of less starting materials. In some embodiments, the compositions of the present disclosure may require about 100 times less basalt than that to use in enhanced silicate rock weathering. Moreover, in many preferred embodiments, the compositions of the present disclosure do not contain harmful organic pollutants that are present in biochar. Moreover, the compositions of the present disclosure can include numerous nutrients. [0097] As such, the methods and compositions of the present disclosure can have various applications. For instance, in some embodiments, the compositions of the present disclosure may be deployed on a large scale (e.g., globally) to capture CO2 from various environments, such as croplands. Moreover, in some embodiments, the methods and compositions of the present disclosure can be utilized to simultaneously enhance the nutrient content of the environment during the capture of CO2.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [0098] In some preferred embodiments, the methods and compositions of the present disclosure can be utilized to simultaneously reduce atmospheric CO2 and increase cropland soil fertility by (a) sequestering mineral bound refractory carbon in the soil, and (b) producing soluble bicarbonate ion (HCO3-) that has a mean residence time of 10,000 years in the ocean. In some embodiments, large- scale deployment of the compositions of the present disclosure material on cropland around the globe could result in removing billions of tons of atmospheric CO2 per year while improving soil fertility, decreasing soil acidity, increasing soil carbon, and increasing soil water content. [0099] Additional embodiments [00100] Reference will now be made to more specific embodiments of the present disclosure and experimental results that provide support for such embodiments. However, Applicant notes that the disclosure below is for illustrative purposes only and is not intended to limit the scope of the claimed subject matter in any way. [00101] Example 1. Alteration of basalt [00102] The kinetics of weathering of basalt is extremely slow (Strefler et al., 2018). For instance, the overall dissolution rate for basalt crushed to 20 µm is ~3 x 10-11 mol m2 s-1 at a pH of 7. The weathering rate increases at low pH and at high temperature. For basalt glass that is hydrothermally altered at 200 ˚C in 100 mM acetic acid (pH = 4.63), the dissolution rate is about ~5 x 10-8 mol m2 s-1 (Peretyazhko et al., 2016) or about 1000-times faster than at room temperature. This example uses crystalline Mt. Holyoke Basalt (diameter = 600-1000 µm; BET surface area = 1.57 m2 g-1) to evaluate dissolution rates in terms of release of Ca2+, Mg2+, Na+, K+ ions with de-ionized water, 100 mM acetic acid, 100 mM citric acid, 100 mM pyroligneous acid (wood vinegar, ~50% acetic acid), and 100 mM HNO3 at 200 ˚C (Table 1). This example shows in that comparison to nitric acid, citric acid and especially the acetic is highly effective in partially altering the basalt and releasing alkali and alkaline earths. Table 1. Log of release rates (in mol m2 s-1) of Ca2+, Mg2+, Na+, K+ ions from Mt. Holyoke Basalt.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 Ca Ca Mg Mg Na Na K K Expt-1 Expt-2 Expt-1 Expt-2 Expt-1 Expt-2 Expt-1 Expt-2 DI water -10.59 -10.44 -11.21 -11.45 -10.89 -10.21 -11.21 -11.45 acetic -8.87 -8.92 -10.76 -10.85 -9.74 -9.96 -10.76 -10.85 citric -9.06 -9.12 -11.02 -11.01 -9.94 -10.26 -11.02 -11.01 pyroligneous -10.00 -10.06 -10.98 -11.24 -9.86 -10.12 -10.98 -11.24 HNO3 -8.83 -8.86 -11.19 -10.91 -9.82 -9.87 -11.19 -10.91 [00103] Example 2. Use of Fortified Biochar to Remove CO2 and Improve Soil Fertility [00104] This Example seeks to evaluate the potential of a novel nutrient-and carbon- rich soil amendment to sequester atmospheric CO2. In particular, Applicant has synthesized a novel soil amendment that is an organo-mineral composite, constituting biochar that is fortified with altered basalt (ABFB), whose application to soils sequesters atmospheric CO2. Additionally, this amendment is expected to improve soil fertility by providing nutrients to soils, decreasing soil acidity, increasing soil carbon, and increasing soil water content. [00105] Example 2.1. ABFB synthesis [00106] Applicant synthesized ABFB by reacting basalt powder with 100 mM acetic acid in an anoxic chamber at 200 °C for 24 h and then by mixing the resulting slurry with biochar prepared by pyrolysis of pine needles at 650 °C. Without being bound by theory, ABFB preparation is based on the following concepts: (a) energy and wood vinegar (~50% acetic acid) generated during pyrolysis of biomass to create biochar can be used to accelerate basalt weathering rate; (b) alteration of basalt with dilute acetic acid produces secondary clay minerals (Fe/Mg smectite) (Peretyazhko et al., 2016) and releases plant nutrients (Ca, Mg, K, P, S, Fe, Cu, Zn, Mn); (c) mixing altered basalt with biochar increases pH (~7.5), thereby promoting iron-oxyhydroxides precipitation, allowing sorption of organics on clay minerals; (d) heating of the mixture combined with iron-oxyhydroxides precipitation causes degradation of polycyclic aromatic hydrocarbon (PAHs) (Jia et al., 2014, Kołtowski and Oleszczuk, 2015), and (e) nutrients released from altered basalt fortify the biochar, which itself is a source of N as well as K and P that also come from basalt alteration. The ABFB is thus a novel soil amendment constituting organo-clay and organo-Fe-oxyhydroxide complexes whose application to soils would engender CO2 removal (CDR) and improve productivity.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00107] Example 2.2. Amendment of soil with ABFB [00108] Without being bound by theory, Applicant envisions that amendment of soil with ABFB can lead to proliferation of bacteria and arbuscular mycorrhizal fungi (Warnock et al., 2007) and accumulation of additional carbon in less decomposable fungal biomass. Second, at a slightly alkaline pH, both smectite and biochar will have a negative surface charge, allowing sorption of cations and some organic moieties. Additionally, these systems will be close to the point of zero charge of iron-oxyhydroxides and promote retention of negatively charged organic moieties and nutrients (e.g., phosphate) (Joseph et al., 2018, Shepherd et al., 2017b). Finally, ABFB would also engender CDR directly through highly refractory carbon in biochar and through the formation of bicarbonate ions. Soil amendments with ABFB would thus lead to a multipronged carbon sequestration: (a) in the soil—sequestration of highly aromatic refractory carbon, carbon adsorbed by iron-oxyhydroxides, carbon occluded by clay-minerals; and (b) in groundwater—release as dissolved bicarbonate ion which could eventually be transported to the ocean where its mean residence time is about 10,000 years. [00109] As illustrated in FIGS. 2A-2B, Applicant demonstrated that ABFB enhanced soil fertility for growing moong beans. FIG.2A shows different samples of three weeks old moong beans in amended Windsor Loam soil of the Connecticut River Valley collected from the Dartmouth Organic Farm. The control soil contains 0.9% Carbon and has a pH of 6.07. The soil was air-dried, sieved, and homogenized. Thereafter, the soil was amended with basalt, hydrothermally altered basalt, ABFB, and biochar. It was then packed on Biorad columns as shown. [00110] The ABFB and biochar amendments increased the carbon content of the soil to 3.62% and 4.93%, respectively. The total mass of soil (plus amendments) in each column was 180 g. Moong beans sprouted in de-ionized water were planted in each of the columns. Precise volumes of de-ionized water were passed through the columns and effluents collected and analyzed for nutrients, major, and trace metals. The plants grew in artificial light (9:15 :: light:dark cycle). [00111] FIG.2B shows the roots of the plants in FIG.2A. The images demonstrate that Moong bean plants grown with ABFB had the best developed roots, the longer trunks, and the larger leaves.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00112] Table 2 provides the calculated C and N concentrations in amended soils in FIG.2A. The table then summarizes the molar ratio of the nutrients (K, N, P) released in effluent over those released by control soil, effluent pH and alkalinity from each of the amended soils. As indicated in Table 2, the soil containing ABFB column releases the highest alkalinity. The median pH of the effluent from the ABFB column (= 7.67) indicates that the bulk of the alkalinity is in the form of bicarbonate ion. The ABFB amended soil released the highest amounts of K and P compared to those amended with basalt, altered basalt, or biochar. The ABFB amended soil also retained its N in comparison to soil with other amendments. These effluent characteristics are the possible reasons for increased soil fertility of ABFB amended soil compared to others. Table 2. Carbon and nitrogen contents of amended soil, release of K, N, and P from soil, its pH and estimated Alkalinity (in equivalent L-1). C N K N P pH Alkalinity (wt%) (wt%) Basalt + Soil 0.87 0.07 3.1 33.3 0.78 7.46 6 Altered basalt 0.7 1.17 6 + Soil 0.87 0.07 1.32 7.30 ABFB + Soil 3.62 0.11 239 0.49 2.15 7.67 26 Biochar + Soil 4.93 0.13 75 0.96 1.88 8.17 16 [00113] Example 2.3. Discussion [00114] In sum, hydrothermal alteration of basalt using low molecular weight organic acids (such as pyroligneous, acetic, citric, and oxalic acids) can accelerate basalt weathering rate by 100- to 1000-fold. This process alters basalts into secondary clay minerals and releases plant nutrients (Ca, Mg, K, P, S, Fe, Cu, Zn, Mn). Mixing altered basalt with biochar allows sorption of organic on clay minerals. Additionally, mixing of alkaline biochar promotes solution pH shifts to >7 allowing precipitation of iron-oxyhydroxides that further trap organics.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00115] Nutrients released from altered basalt fortify the biochar, which itself is a source of K, N, and P. The resulting slurry of altered basalt with fortified biochar (ABFB) is a novel soil amendment constituting an organo-clay composite whose application to soils would sequester atmospheric CO2 both on land and in the ocean. In Applicant’s experiments, for 10 g of ABFB added to soil, about 5 g carbon would be sequestered in soil and 0.32 g carbon would be sequestered as bicarbonate in the ocean. Thus, it is expected that about 0.5 tons of CO2 would be removed per ton of ABFB applied per year. [00116] Additionally, application of ABFB is expected to improve soil fertility by providing nutrients to soils, decreasing soil acidity, increasing soil carbon, and increasing water content. Applicant’s experiments also show that ABFB is a better solution than just basalt, altered basalt, or biochar in improving soil fertility. As such, ABFB has the potential to be deployed in the field and on a large scale to remove atmospheric CO2. [00117] Example 3. Production of ABFB [00118] This Example provides various processes for generating ABFB. For instance, FIG.3 illustrates the production of ABFB using electricity generated from syngas, where the syngas is produced by a biochar producing gasifier (i.e., an All Power Labs PP30 Power Pallet gasifier). Biomass (e.g., wood shavings) is first placed in a gasifier to generate biochar through pyrolysis at ≥ 650 ˚C. Syngas produced as a byproduct is utilized to generate electricity. [00119] The electricity generated from the engine is then used to grind basalt into a powder form and sieve it to obtain the adequate size. The ground basalt is then placed in a reactor with dilute acetic/citric acid (i.e., a Buechiglas kiloclave® lab pressure reactor). The reactor is powered by the electricity generated during biochar production, also using the steam produced due to the combustion of syngas. The basalt is hydrothermally altered in the reactor at around 200 °C. Finally, the altered basalt is mixed with the produced biochar in the reactor and heated to 120 °C using electricity and hot water from gasifier to form ABFB (i.e., fortified biochar in a slurry)| [0003] PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00120] FIG. 4 illustrates another ABFB production process that can be streamlined by deploying two reactors (i.e., two Buechiglas kiloclave® lab pressure reactors). The electricity generated from the engine attached to a gasifier (i.e., an All Power Labs PP30 Power Pallet gasifier) is used to grind basalt into a powder form and sieve it to obtain the adequate size. The ground basalt is then placed in Reactor-1 with dilute acetic/citric acid. The reactor is powered by the electricity generated during biochar production, also using the steam produced due to the combustion of syngas. The basalt is hydrothermally altered in Reactor-1 at around 200 °C. The altered basalt is then mixed with the produced biochar in Reactor-2 and heated to 120 °C using electricity and steam from gasifier to form ABFB (i.e., fortified biochar in a slurry). [00121] Different gasifiers and reactors may be used to scale up ABFB production to take advantage of the economy of scale. The formed ABFB may then be processed in various manners. For instance, the ABFB may be dried for spreading on land through the utilization of existing equipment. It may also be pelletized, if needed. The ABFB may be spread as a slurry using existing equipment after modifying its consistency to use with slurry spreading equipment. [00122] FIG.5 illustrates another ABFB production process that involves the following steps. First, basalt is ground to about 20 µm. The powdered basalt is then mixed with wood vinegar in water and heated at 200 °C for 24 hours. Finally, biochar produced from pine needles at 650 °C is homogenized with the powdered and altered basalt at 120 °C and a pH of 7 to form ABFB. [00123] FIG.6 illustrates another ABFB production process that involves the following steps. First, basalt is ground to about 20 µm. In parallel, biochar is produced by heating at 450 °C in a self- heated oven with wood vinegar as the by-product. The powdered basalt is then mixed with wood vinegar in water and heated at 200 °C. In some embodiments, the biochar is heated in an oven at 650 °C and mixed with altered basalt and homogenized. In other embodiments, biochar produced by heating at 450 °C in a self-heated oven is added directly to the altered basalt and homogenized to form ABFB. [00124] FIG.7 illustrates another ABFB production process that involves using Deccan basalt from India. The basalt is initially ground to 200-800 µm. The powdered basalt is then mixed with wood vinegar in water and heated at 200 °C. Finally, commercial biochar produced at 450 °C in a self-heated oven is sieved to 200-800 µm and homogenized with the powdered and altered basalt at 120 °C and a pH of 7.5 to form ABFB.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00125] FIG. 8 shows an image of an ABFB formed in accordance with the methods of the present disclosure. [00126] References [00127] AMONETTE, J. E., BLANCO-CANQUI, H., HASSEBROOK, C., LAIRD, D. A., LAL, R., LEHMANN, J. & PAGE-DUMROESE, D.2021. Integrated biochar research: A roadmap. Journal of Soil and Water Conservation, 76, 24A-29A. [00128] BEERLING, D. J., EPIHOV, D. Z., KANTOLA, I. B., MASTERS, M. D., REERSHEMIUS, T., PLANAVSKY, N. J., REINHARD, C. T., JORDAN, J. S., THORNE, S. J. & WEBER, J.2024. Enhanced weathering in the US Corn Belt delivers carbon removal with agronomic benefits. 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Potential and costs of carbon dioxide removal by enhanced weathering of rocks. Environmental Research Letters, 13. [00159] TAYLOR, L. L., QUIRK, J., THORLEY, R., KHARECHA, P. A., HANSEN, J., RIDGWELL, A., LOMAS, M. R., BANWART, S. A. & BEERLING, D. J.2016. Enhanced weathering strategies for stabilizing climate and averting ocean acidification. Nature Climate Change, 6, 402-406. [00160] WARNOCK, D. D., LEHMANN, J., KUYPER, T. W. & RILLIG, M. C.2007. Mycorrhizal responses to biochar in soil–concepts and mechanisms. Plant and soil, 300, 9-20. [00161] WILSON, M.1989. Igneous petrogenesis, Springer. [00162] WINTER, J. D.2014. Principles of igneous and metamorphic petrology, Pearson education Harlow, UK. [00163] WOOLF, D., AMONETTE, J. E., STREET-PERROTT, F. A., LEHMANN, J. & JOSEPH, S.2010. Sustainable biochar to mitigate global climate change. Nature Communications, 1. [00164] XIA, L., CAO, L., YANG, Y., TI, C., LIU, Y., SMITH, P., VAN GROENIGEN, K. J., LEHMANN, J., LAL, R. & BUTTERBACH-BAHL, K.2023. Integrated biochar solutions can achieve carbon-neutral staple crop production. Nature Food, 4, 236-246.PCT Application Attorney Docket No. AF60544.P046WO Dartmouth Ref. No.2023-035-04 [00165] XIAO, X., CHEN, B., CHEN, Z., ZHU, L. & SCHNOOR, J. L.2018. Insight into multiple and multilevel structures of biochars and their potential environmental applications: a critical review. Environmental science & technology, 52, 5027-5047. [00166] YANG, Y., SUN, K., HAN, L. F., JIN, J., SUN, H. R., YANG, Y. & XING, B. S.2018. Effect of minerals on the stability of biochar. Chemosphere, 204, 310-317. [00167] Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the present disclosure to its fullest extent. The embodiments described herein are to be construed as illustrative and not as constraining the remainder of the disclosure in any way whatsoever. While the embodiments have been shown and described, many variations and modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. Accordingly, the scope of protection is not limited by the description set out above, but is only limited by the claims, including all equivalents of the subject matter of the claims. The disclosures of all patents, patent applications and publications cited herein are hereby incorporated herein by reference, to the extent that they provide procedural or other details consistent with and supplementary to those set forth herein. Family Number|(111908782)|111908782|Abstract|(WO2024220896 A3)|Des modes de réalisation de la présente divulgation concernent une composition qui comprend au moins un basalte et au moins un biocharbon. Les biocharbon peut comprendre du biocharbon enrichi en nutriments, les nutriments étant dérivés du basalte. Des modes de réalisation supplémentaires de la présente divulgation concernent des procédés de capture de CO2 dans un environnement par exposition de l'environnement à une composition de la présente divulgation. Les compositions de la présente divulgation peuvent également améliorer le contenu nutritif de l'environnement. D'autres modes de réalisation de la présente divulgation concernent des procédés d'amélioration de la fertilité du sol par application d'une composition de la présente divulgation au sol. Des modes de réalisation supplémentaires concernent des procédés de fabrication d'une composition par altération d'au moins un basalte et mélange du basalte altéré avec au moins un biocharbon.|IPC codes|(WO2024220896 A3)|B01D-053/46|B01D-053/62|B01J-020/02|B01J-020/20|C01B-032/05|Title|(WO2024220896 A2)|Carbon dioxide removal with biochar fortified by accelerated weathering of basalt (abfb)|Élimination de dioxyde de carbone avec biocharbon enrichi par altération accélérée de basalte (abfb)|(WO2024220896 A3)|Carbon dioxide removal with biochar fortified by accelerated weathering of basalt (abfb)|Élimination de dioxyde de carbone avec biocharbon enrichi par altération accélérée de basalte (abfb)| Chemical engineering|Environmental technology|Materials, metallurgy C05D-009/02|C05F-005/00/2 C05D-009/02|C05F-005/00/2 B01D-053/46|B01D-053/62|B01J-020/02|B01J-020/20|C01B-032/05 B01D-053/46|B01D-053/62|B01J-020/02|B01J-020/20|C01B-032/05 US20240116093|US11560322|WO202248787|US10766827 US20240116093 109200926 WHO=Examiner SELF=N CAT=P CAT=A|US11560322 103518653 WHO=Examiner SELF=N CAT=A|WO202248787 92984336 WHO=Examiner SELF=N CAT=A|US10766827 90465882 WHO=Examiner SELF=N CAT=A XP093268281; US10766827; US11560322; WO202248787; US20240116093 (WO2024/220896)|International Search Report [Examiner]|-BUSS WOLFRAM, YEATES KIRSTY, ROHLING EELCO J, BOREVITZ JUSTIN: "Enhancing natural cycles in agro-ecosystems to boost plant carbon capture and soil storage", OXFORD OPEN CLIMATE CHANGE, vol. 1, no. 1, 26 May 2021 (2021-05-26), pages 1 - 13, XP093268281, ISSN: 2634-4068, DOI: 10.1093/oxfclm/kgab006| PENDING (WO2024/220896)|PENDING ALIVE (WO2024/220896)|ALIVE (WO2024/220896)|LEGAL DETAILS FOR WO2024/220896|Actual or expected expiration date=2026-10-19|Legal state=ALIVE|Status=PENDING|Event publication date=2024-04-19|Event code=WO/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=WO WOUS2024/025537|Application date=2024-04-19|Standardized application number=2024WO-US25537|Event publication date=2024-10-24|Event code=WO/A2|Event group=Examination events|International application published with declaration under Article 17 (2) (a)|Publication country=WO|Publication number=WO2024/220896|Publication stage code=A2|Publication date=2024-10-24|Standardized publication number=WO2024220896|Event publication date=2025-01-23|Event code=WO/A3|Event indicator=Pos|Event group=Examination events|Later publication of ISR with revised front page|Publication country=WO|Publication number=WO2024/220896|Publication stage code=A3|Publication date=2025-01-23|Standardized publication number=WO2024220896|MEMBER STATE LEGAL DETAILS FOR DE|Actual or expected expiration date=2025-11-20|Legal state=DEAD|Status=LAPSED|Corresponding cc:|Designated or member state=DE|Event publication date=2025-11-20|Event code=WO/NENP|Event group=Event indicating Not In Force|Non-entry into the national phase|Corresponding cc:|Designated or member state=DE|MEMBER STATE LEGAL DETAILS FOR EP|Actual or expected expiration date=2026-04-15|Legal state=DEAD|Status=LAPSED|Corresponding cc:|Designated or member state=EP Corresponding appl: EP24793632|Event publication date=2026-04-15|Event code=WO/122|Event indicator=Neg|Event group=Event indicating Not In Force|EP: PCT app. not ent. europ. phase|EP: PCT anmeldung nicht in europaeische phase eingetreten|Corresponding cc:|Designated or member state=EP (WO2024/220896)|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW|(WO2024/220896)|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ|(WO2024/220896)|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR|(WO2024/220896)|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML|(WO2024/220896)|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (WO2024/220896)|WO https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCDC5aqeOt6q4ANwwKC8dCjRkaV0SMUACwOCCKReMmHu7M9Ry4MrhQjLALkMBz8hwaI=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006680437&ekey=2301&xpn=WO2024220896&kind=A3 http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2024220896&redirectedID=true https://permalink.orbit.com/RenderStaticFirstPage?XPN=tDFZKzXudXGuciYsiNrJ4rmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT US (WO2024/220896)|US|(WO2024/220896)|US (WO2024/220896)|NAME=TRUSTEES OF DARTMOUTH COLLEGE 11 Rope Ferry Road, #6210 Hanover, NH 03755-1404 , COUNTRY=US|(WO2024/220896)|NAME=TRUSTEES OF DARTMOUTH COLLEGE 11 Rope Ferry Road, #6210 Hanover, NH 03755-1404 , COUNTRY=US (WO2024/220896)|US|(WO2024/220896)|US (WO2024/220896)|NAME=AMINI, Farhang Shackelford, Bowen, Mckinley & Norton, LLP 717 Texas Avenue, Suite 2700 Houston, TX 77002 , POSTCODE=77002 , COUNTRY=US|(WO2024/220896)|NAME=AMINI, Farhang Shackelford, Bowen, Mckinley & Norton, LLP 717 Texas Avenue, Suite 2700 Houston, TX 77002 , POSTCODE=77002 , COUNTRY=US (WO2024/220896)|US|(WO2024/220896)|US (WO2024/220896)|NAME=SHARMA, Mukul c/o Trustees Of Dartmouth College 11 Rope Ferry Road, #6210 Hanover, NH 03755-1404, POSTCODE=03755-1404, COUNTRY=US|(WO2024/220896)|NAME=SHARMA, Mukul c/o Trustees Of Dartmouth College 11 Rope Ferry Road, #6210 Hanover, NH 03755-1404, POSTCODE=03755-1404, COUNTRY=US 0 1 Titre: (WO2024/220896)|Carbon dioxide removal with biochar fortified by accelerated weathering of basalt (abfb) Résumé: (WO2024/220896)|Embodiments of the present disclosure pertain to a composition that includes at least one basalt and at least one biochar. The biochai- may include nutrient fortified biochar, where the nutrients are derived from the basalt. Additional embodiments of the present disclosure pertain to methods of capturing CO2 from an environment by exposing the environment to a composition of the present disclosure. The compositions of the present disclosure may also enhance the nutrient content of the environment. Further embodiments of the present disclosure pertain to methods of enhancing soil fertility by applying a composition of the present disclosure to the soil. Additional embodiments pertain to methods of making a composition by altering at least one basalt and mixing the altered basalt with at least one biochar. 85 Abstract gpt-4o-mini no The focus is on biochar and its nutrient enhancement rather than directly on accelerated weathering for CO2 capture.
88 CN202210333976 CN202210333976 CN114735664|CN114735664 100868601 CN114735664 B 2023-05-30 [CN114735664B]|CN114735664 A 2022-07-12 [CN114735664] 2022-03-30 2022-03-30 2023-05-30|2022-07-12 (CN114735664B)|2023-05-30 (CN114735664)|2042-03-30 (CN114735664)|Automatic acid washing device and method for producing cubic boron nitride (CN114735664)|The invention provides a novel automatic acid washing device for cubic boron nitride production. The novel automatic acid washing device for cubic boron nitride production comprises a box body, a treatment box, a filter box and a crushing and weighing mechanism, the treatment box is arranged on the top of the box body, the filter box is arranged on the outer wall of one side of the box body, and the crushing and weighing mechanism is arranged on the treatment box; and the crushing and weighing mechanism comprises two rotating rods, two crushing rollers, a connecting motor, a first filtering plate, a rotating column, a first servo motor, a funnel, a storage box, a weighing sensor, a placing plate and a circulating assembly, and the two rotating rods are rotationally mounted in the treatment box. The novel automatic acid washing device and method for cubic boron nitride production provided by the invention have the advantages that the acid washing and carbon removal effects can be enhanced, so that the harm to the bodies of staff can be avoided while safe purification can be performed on cubic boron nitride. ZHENGZHOU ZHONGNAN JETE SUPERABRASIVES (CN114735664)|ZHENGZHOU ZHONGNAN JETE SUPERABRASIVES CO. LTD. ([CN])|(CN114735664)|ZHENGZHOU ZHONGNAN JETE SUPERABRASIVES CO. LTD. ([CN]) WANG YONGKAI|ZHANG XIANGFA|WEI XING|WANG DAPENG|LU CUILIAN|LIU ZHANGJIANG|ZHANG XIANGXIANG (CN114735664)|WANG YONGKAI|ZHANG XIANGFA|WEI XING|WANG DAPENG|LU CUILIAN|LIU ZHANGJIANG|ZHANG XIANGXIANG|(CN114735664)|WANG YONGKAI|ZHANG XIANGFA|WEI XING|WANG DAPENG|LU CUILIAN|LIU ZHANGJIANG|ZHANG XIANGXIANG (CN114735664)|ZHANG LEI;Shenzhen Shenhui Zhicheng Patent Agency (general partnership)|Reg. Nb: 44725 (CN114735664)|Therefore, there is a need to provide a new automatic acid cleaning device and method for cubic boron nitride production, which solve the above technical problems.| (CN114735664)|1. An automatic acid cleaning device for cubic boron nitride production, which is characterized by comprising: the device comprises a box body, a processing box, a filtering box and a crushing weighing mechanism, wherein the processing box is arranged on the top of the box body, the filtering box is arranged on the outer wall of one side of the box body, and the crushing weighing mechanism is arranged on the processing box; the crushing weighing mechanism comprises two rotating rods, two crushing rollers, a connecting motor, a first filter plate, a rotating column, a first servo motor, a funnel, a storage box, a weighing sensor, a placing plate and a circulating assembly, wherein the two rotating rods are rotatably installed in the treatment box, one end of each corresponding rotating rod extends out of one side of the treatment box, the two crushing rollers are arranged in the treatment box, the two crushing rollers are fixedly installed on the two rotating rods respectively, the two crushing rollers are meshed, the connecting motor is fixedly installed on one side outer wall of the treatment box, an output shaft of the connecting motor is fixedly connected with one end of each corresponding rotating rod, the first filter plate is arranged in the treatment box, the rotating column is rotatably installed in the treatment box, the rotating column is positioned below the first filter plate, one side of the rotating column extends out of one side of the treatment box, the first servo motor is fixedly installed on one side outer wall of the treatment box, an output shaft of the first servo motor is fixedly connected with one side outer wall of the rotating column, the funnel is arranged in the treatment box, the first filter plate is fixedly connected with one side outer wall of the corresponding rotating column, the weighing sensor is fixedly connected with the first filter plate, the weighing sensor is arranged on the bottom of the storage box, the weighing sensor is fixedly arranged on the top of the storage box, and the weighing sensor is fixedly arranged on the top of the storage box; the circulating assembly is arranged on the treatment box; the heating device comprises a box body, and is characterized in that a stirring heating mechanism is arranged on the box body and comprises a first connecting pipe, a first conical gear, a third servo motor, a second conical gear, a first hollow plate, a second connecting pipe, a second hollow plate, four heating pipes, a heating layer and heating wires, wherein the first connecting pipe is rotatably arranged on the inner wall of the top of the box body, the top end of the first connecting pipe extends to the upper part of the top of the box body, the first conical gear is fixedly sleeved on the first connecting pipe, the first conical gear is positioned above the top of the box body, the third servo motor is fixedly arranged on the top of the box body, the second conical gear is fixedly arranged on an output shaft of the third servo motor, the second conical gear is meshed with the first conical gear, the first hollow plate is arranged in the box body, the first hollow plate is fixedly arranged on the bottom end of the first connecting pipe, the second connecting pipe is fixedly arranged on the bottom of the first hollow plate, the second hollow plate is fixedly arranged on the bottom of the second hollow plate, the fourth heating pipe is fixedly arranged on the bottom of the fourth heating pipe, and the heating wire is arranged in the hollow heating layer.| (CN114735664)|The invention also provides an automatic acid washing method for producing the cubic boron nitride, which comprises the following steps of:|The invention discloses an automatic acid washing device for producing cubic boron nitride, which comprises an acid washing barrel, wherein a stirring mechanism is arranged in the acid washing barrel, a plastic filter barrel is arranged above the stirring mechanism, a support column is vertically arranged at the right end in the acid washing barrel, the upper end of the support column is hinged with the right end of the plastic filter barrel, a lifting mechanism is arranged at the upper end of the acid washing barrel, a plastic rope connected with the left end of the plastic filter barrel is arranged at the upper end of the plastic filter barrel, a first water inlet pipe is arranged at the upper end of the plastic filter barrel, a discharging funnel is coaxially arranged at the right end of the plastic filter barrel, the first water inlet pipe is arranged at the upper end of the plastic filter barrel, an automatic acid washing device for producing cubic boron nitride is arranged at the upper end of the plastic filter barrel, a first water outlet pipe is arranged at the upper end of the lower end of the plastic filter barrel, and an automatic acid washing pipe is arranged at the lower end of the plastic filter barrel.|The invention provides an automatic acid washing device for producing cubic boron nitride.| (CN114735664)|BORON NITRIDE(100,43)|CUBIC BORON NITRIDE(100,30)|AUTOMATIC ACID(100,14)|BORON NITRIDE PRODUCTION(100,11)|PLASTIC FILTER BARREL(100,10)|CONICAL GEAR(88,22)|TREATMENT BOX(80,35)|ACID WASHING BARREL(77,4)|SERVOMOTOR(73,40)|ROTATING COLUMN(58,23)|AUGER(54,39)|STORAGE BOX(54,22)|PROCESSING BOX(54,17)|TRANSPORTATION PIPE(54,10)|ROTATING ROD(52,24)|HOLLOW PLATE(49,27)|CRUSHING(49,15)|FILTER PLATE(46,18)|ELECTROMAGNETIC VALVE(43,18)|HEAT PIPE(43,8)|DISCHARGING FUNNEL(43,1)|FILTERING BOX(41,3)|CIRCULATION(40,10)|FILTER BOX(39,15)|FUNNEL(37,13)|BOX FILTERING(34,5)|AUTOMATIC ACID WASHING(31,4)|DISCHARGING PIPE(31,3)|CREAM YELLOW(30,6)|PLASTIC ROPE(30,1)|CONVEYING PIPE(29,7)|FEEDER HOPPER(28,2)|CONNECTING PIPE(27,33)|HEATING WIRE(26,8)|ROSE BOX(25,10)|SUPPORT COLUMN(25,2)|SHELL(24,18)|PORT COOPERATION(24,2)|DRIVING MOTOR(23,15)|MILKY YELLOW(23,2)|CRUSHING ROLLER(22,4)|BREAKING ROLLER(22,2)|WATER INLET PIPE(22,2)|FILLING TUBE(21,4)|OBSERVATION WINDOW(21,4)|SOLENOID VALVE(20,9)|DISCHARGE HOLE(20,4)|LIQUID DISCHARGE PIPE(20,4)|BEVEL GEAR(19,9)|DISCHARGING OPENING(19,5)|TRANSPORTATION EQUIPMENT(19,3)|PLATE POSITION(18,6)|STAFF(18,6)|CONVEYING EQUIPMENT(18,2)|ANNULAR GUIDE BLOCK(17,10)|FEED HOPPER(17,4)|REDDISH BROWN GAS(17,3)|HEATING PIPE BOTTOM(17,2)|SEALING LID(17,2)|OUTPUT SHAFT(15,27)|BLAST PIPE(15,4)|ACIDIC WASH(15,3)|STOPPING HEATING(15,3)|WATER OUTLET PIPE(15,1)|TREATMENT BOX SIDE(14,10)|DISCHARGE GATE(14,4)|HARM(14,3)|PLASTIC FILTER BARREL END(14,2)|DISCHARGE OPENING(13,5)|HEAT LAYER(13,4)|PROGRAMMABLE LOGIC CONTROLLER(11,36)|BIN(11,2)|CARBONIZING REACTION(11,2)|ACID TREATMENT(10,3)|DROPWISE(10,3)|WHITE SMOKE(10,3)|FEED OPENING(10,2)|UNQUALIFIED BROKEN MATERIAL(10,2)|PROCESSING BOX BOTTOM(9,1)|NITRIC ACID(8,11)|BAFFLE PLATE(8,7)|WEIGHED MATERIAL(8,3)|ACID WATER(8,2)|TRANSPORT PIPE(7,3)|HOLLOW SLAB(7,2)|SAFETY PURIFICATION(7,2)|OUTER WALL(6,19)|GUIDING MATERIAL(6,3)|FLAMMABLE SUBSTANCE(6,1)|INNER WALL(5,14)|CUBIC BORON NITRIDE PRODUCTION(5,2)|STIRRING RAW MATERIAL(5,2)|EXPLOSIVE SUBSTANCE(5,1)|MATURE BOLT(5,1)|OXIDANT PERCHLORIC ACID(5,1)|PERSON PROGRAMMING(5,1)|RIGHT END(5,1)|SCREENING ROLE(5,1)|TEMPERATURE SENSOR(4,5)|EXHAUST PIPE(4,4)|ANNULAR MATERIAL GUIDING BLOCK(4,3)|DISCONTINUOUS MATERIAL(4,3)|GRAPHITE(4,3)|LIGHT GREEN(4,3)|ROOM TEMPERATURE(4,3)|TREATMENT TANK(4,2)|BROWN REACTION(4,1)|INTERMESHING ACTION(4,1)|ROSE BOX MOUNTING(4,1)|OUTER WALL SIDE(3,14)|MATERIAL GUIDE PLATE(3,9)|DRIVING MOTOR OUTPUT SHAFT(3,5)|BORON NITRIDE FALL(3,1)|BROWN CARBON SOLUTION(3,1)|CONCENTRATE(3,1)|COOPERATION(3,1)||(CN114735664)|BORON NITRIDE(100,42)|AUTOMATIC ACID WASHING(100,23)|ACID WASHING(100,18)|BORON NITRIDE PRODUCTION(100,16)|AUTOMATIC ACID(100,3)|PROCESSING BOX(62,31)|CUBIC BORON NITRIDE(59,26)|SERVOMOTOR(52,37)|FILTER BOX(52,25)|ROTATING COLUMN(49,27)|CIRCULATION SUBASSEMBLY(45,2)|TRANSPORTATION PIPE(43,16)|PIECE LOCATION(43,14)|ELECTROMAGNETIC VALVE(41,17)|ROTATING ROD(40,20)|BULL STICK(40,2)|STORAGE BOX(39,19)|FUNNEL(38,21)|CRUSHING(38,14)|FILTER PLATE(35,16)|DUMP BODY BOARD(33,10)|HEAT PIPE(31,12)|BEVEL GEAR(28,29)|CIRCULATION(27,6)|TREATMENT BOX(25,16)|CONVEYING PIPE(25,5)|INCASEMENT(25,2)|HOLLOW PLATE(23,24)|FEEDER HOPPER(23,2)|PLACING PLATE(22,4)|STOCK GUIDE(22,2)|HEATING WIRE(21,9)|HARM(21,3)|ACIDIC WASH(20,9)|STAFF(20,6)|CRUSHING ROLLER(19,4)|DISCHARGE PORT(19,4)|OBSERVATION WINDOW(18,4)|REMOVING CARBON(18,3)|DISCHARGING PIPE(18,2)|BROKEN WEIGHING MACHINE CONSTRUCT(18,1)|CONNECTING PIPE(17,37)|ANNULAR GUIDE BLOCK(17,8)|FILLING TUBE(17,4)|LIQUID DISCHARGE PIPE(17,4)|FEED OPENING(16,10)|PACKING AUGER(16,7)|CONVEYING EQUIPMENT(16,2)|SOLENOID VALVE(15,16)|FEED HOPPER(15,4)|TRANSPORTATION EQUIPMENT(15,3)|SEALING LID(15,2)|ROTATION POST(15,1)|SHELL(14,15)|REDDISH BROWN GAS(14,3)|EXHAUST PIPE(13,9)|MIXED ACID(13,7)|HEATING ZONE(13,5)|BLAST PIPE(13,4)|OUTPUT SHAFT(12,29)|BIN(12,7)|ANNULAR ARRAY(12,3)|CRUSHED UNQUALIFIED MATERIAL(12,3)|STOPPING HEATING(12,3)|PLATE POSITION(11,7)|COMPONENT LOCATION(11,2)|CONVEYER(11,2)|PROCESSING BOX SIDE(10,8)|HEAT LAYER(10,7)|HOLLOW BOARD BOTTOM(10,2)|MAKE THING(10,2)|PROCESSING MOUNTING(10,1)|ROTATING MODE(10,1)|DISCHARGE OPENING(9,2)|CONNECTION MOTOR(9,1)|PLACE BOARD(9,1)|OUTER WALL(8,23)|ACID TREATMENT(8,3)|BAFFLE PLATE(8,3)|TRANSPORTATION SUBASSEMBLY(8,2)|PROGRAMMABLE LOGIC CONTROLLER(7,36)|NITRIC ACID(7,11)|PROCESSING DISPLAY CASE(7,3)|RAW MATERIAL(6,25)|PLASTIC FILTER CYLINDER(6,6)|WEIGHED MATERIAL(6,3)|ACIDIC WATER FALL(6,1)|AUGER ADAPTATION(6,1)|MOVING ROW MATERIAL PIPE(6,1)|INNER WALL(5,18)|LIGHT GREEN(5,6)|FEED PIPE(5,5)|TREATMENT BOX SIDE(5,5)|MATERIAL GUIDE ROLE(5,3)|CASING TOP(5,2)|DISCONTINUOUS MATERIAL(5,2)|DRIVING MOTOR DRIVE(5,2)|FIXED CONNECTION(5,2)|CUBIC NITRIDING(5,1)|FLAMMABLE SUBSTANCE(5,1)|CLAMPING FORCE(4,3)|TREATMENT TANK(4,3)|CIRCULATION MODULE(4,1)|EXPLOSIVE SUBSTANCE(4,1)|HAULAGE EQUIPMENT(4,1)|MACHINING INDUSTRY(4,1)|MATURE BOLT(4,1)|SCREENING ROLE(4,1)|WORKING PERSONNEL(4,1)|TEMPERATURE SENSOR(3,5)|ANNULAR MATERIAL GUIDE BLOCK(3,3)|CENTURY(3,2)|DISCHARGE GATE(3,2)|ALKALI BOILING(3,1)|ALKALI WASHING(3,1)|CUBIC SILICON NITRIDE(3,1)|INTERMESHING ACTION(3,1)|OXIDANT PERCHLORIC ACID(3,1)|PLASTIC ROPE(3,1)|ROSE BOX MOUNTING(3,1)|STIRRING HEATING(3,1)| (CN114735664)|1. An automatic acid cleaning device for cubic boron nitride production, which is characterized by comprising:|the device comprises a box body, a processing box, a filtering box and a crushing weighing mechanism, wherein the processing box is arranged on the top of the box body, the filtering box is arranged on the outer wall of one side of the box body, and the crushing weighing mechanism is arranged on the processing box;|the crushing weighing mechanism comprises two rotating rods, two crushing rollers, a connecting motor, a first filter plate, a rotating column, a first servo motor, a funnel, a storage box, a weighing sensor, a placing plate and a circulating assembly, wherein the two rotating rods are rotatably installed in the treatment box, one end of each corresponding rotating rod extends out of one side of the treatment box, the two crushing rollers are arranged in the treatment box, the two crushing rollers are fixedly installed on the two rotating rods respectively, the two crushing rollers are meshed, the connecting motor is fixedly installed on one side outer wall of the treatment box, an output shaft of the connecting motor is fixedly connected with one end of each corresponding rotating rod, the first filter plate is arranged in the treatment box, the rotating column is rotatably installed in the treatment box, the rotating column is positioned below the first filter plate, one side of the rotating column extends out of one side of the treatment box, the first servo motor is fixedly installed on one side outer wall of the treatment box, an output shaft of the first servo motor is fixedly connected with one side outer wall of the rotating column, the funnel is arranged in the treatment box, the first filter plate is fixedly connected with one side outer wall of the corresponding rotating column, the weighing sensor is fixedly connected with the first filter plate, the weighing sensor is arranged on the bottom of the storage box, the weighing sensor is fixedly arranged on the top of the storage box, and the weighing sensor is fixedly arranged on the top of the storage box;|the circulating assembly is arranged on the treatment box;|the heating device comprises a box body, and is characterized in that a stirring heating mechanism is arranged on the box body and comprises a first connecting pipe, a first conical gear, a third servo motor, a second conical gear, a first hollow plate, a second connecting pipe, a second hollow plate, four heating pipes, a heating layer and heating wires, wherein the first connecting pipe is rotatably arranged on the inner wall of the top of the box body, the top end of the first connecting pipe extends to the upper part of the top of the box body, the first conical gear is fixedly sleeved on the first connecting pipe, the first conical gear is positioned above the top of the box body, the third servo motor is fixedly arranged on the top of the box body, the second conical gear is fixedly arranged on an output shaft of the third servo motor, the second conical gear is meshed with the first conical gear, the first hollow plate is arranged in the box body, the first hollow plate is fixedly arranged on the bottom end of the first connecting pipe, the second connecting pipe is fixedly arranged on the bottom of the first hollow plate, the second hollow plate is fixedly arranged on the bottom of the second hollow plate, the fourth heating pipe is fixedly arranged on the bottom of the fourth heating pipe, and the heating wire is arranged in the hollow heating layer.|2. An automatic acid cleaning apparatus for cubic boron nitride production according to claim 1, wherein: the circulating assembly comprises a shell, a second servo motor, a first auger and a material guide plate, wherein the shell is fixedly arranged on the outer wall of one side of the treatment box, the second servo motor is fixedly arranged on the top of the shell, the first auger is rotatably arranged in the shell, the top end of the first auger extends to the upper part of the top of the shell and is fixedly connected with the output shaft of the second servo motor, and the material guide plate is fixedly arranged in the treatment box.|3. An automatic acid cleaning apparatus for cubic boron nitride production according to claim 2, wherein: the inner wall of one side of the treatment box is provided with a first through hole which is communicated with the shell, the first through hole is matched with the first filter plate, the inner wall of one side of the treatment box is provided with a second through hole which is communicated with the shell, and the second through hole is matched with the guide plate.|4. An automatic acid cleaning apparatus for cubic boron nitride production according to claim 1, wherein: the device comprises a processing box, and is characterized in that a positioning assembly is arranged on the processing box and comprises a first positioning block, an annular guide block and a second positioning block, wherein the first positioning block is arranged in the processing box, the first positioning block is positioned at the rear of the storage box and is matched with the storage box, the annular guide block is arranged on the inner wall of the bottom of the processing box and is matched with the storage box, the second positioning block is arranged on the annular guide block and is positioned below the first positioning block, the second positioning block is matched with the storage box, a discharging pipe is fixedly arranged at the bottom of the processing box, a second electromagnetic valve is arranged on the discharging pipe, and the bottom end of the discharging pipe extends into the box.|5. An automatic acid cleaning apparatus for cubic boron nitride production according to claim 1, wherein: the box is provided with a transportation assembly, the transportation assembly comprises a transportation pipe, a driving motor, a baffle and a second auger, the transportation pipe is arranged in the box, the driving motor is fixedly arranged in the transportation pipe, the baffle is fixedly arranged in the transportation pipe, the second auger is arranged in the transportation pipe, the second auger penetrates through the baffle and is rotationally connected with the baffle, one end of the second auger is fixedly connected with an output shaft of the driving motor, and one end of the second auger, far away from the baffle, extends into the filter box.|6. An automatic acid cleaning apparatus for cubic boron nitride production according to claim 5, wherein: the box body is provided with a discharging opening, the discharging opening is communicated with the conveying pipe, the discharging opening is provided with a third electromagnetic valve, the outer wall of one side of the filter box is provided with a third opening, the third opening is communicated with the conveying pipe, and the third opening is matched with the second auger.|7. The automatic acid washing device for cubic boron nitride production according to claim 6, wherein: the filter box is internally provided with a second filter plate, the second filter plate is located below the second auger, a discharge hole is formed in the outer wall of one side of the filter box, conveying equipment is arranged below the bottom of the filter box, a liquid discharge pipe is fixedly arranged at the bottom of the filter box, a fourth electromagnetic valve is arranged on the liquid discharge pipe, a baffle plate is arranged on the outer wall of one side of the filter box, and the baffle plate is matched with the discharge hole.|8. An automatic acid cleaning apparatus for cubic boron nitride production according to claim 1, wherein: the top of handling the case is equipped with the feeder hopper, the top of box is equipped with the filling tube, be equipped with sealed lid on the filling tube, one side outer wall of box is equipped with the blast pipe, be equipped with the fifth solenoid valve on the blast pipe, the top inner wall of box is equipped with temperature sensor, one side outer wall of box is equipped with the PLC controller, be equipped with the observation window on the box.|9. An automatic acid washing method for producing cubic boron nitride is characterized in that: a tank for an automatic acid cleaning device for cubic boron nitride production according to any one of claims 1 to 8, comprising the raw materials:|s1, raw materials:|(1) Cubic boron nitride, mixed acid;|s2, crushing and screening:|(1) Starting a connecting motor to operate through a PLC (programmable logic controller), driving a rotating rod to rotate through an output shaft of the connecting motor, driving crushing rollers to rotate through the rotating rod, enabling two crushing rollers to mutually approach to each other to rotate under the meshing effect, and then throwing cubic boron nitride into a processing box through a feed hopper on the processing box to enable the cubic boron nitride to fall onto the two crushing rollers, so that the cubic boron nitride is crushed oppositely through the two crushing rollers;|(2) Broken material can enter into the funnel through first filter, and first filter then plays the effect of screening, first filter is the mesh, then opens the first solenoid valve on the funnel through the PLC controller, cause the material that filters to enter into the bin through the funnel, make it drop place on the board, and along with placing the material on the board more and more, consequently can extrude weighing sensor under the effect of gravity, thereby weigh through weighing sensor, and show on passing the result to the PLC controller, cause convenient staff to control it, when the material reaches, then can close first solenoid valve through the PLC controller:|(3) The first servo motor is started to operate through the PLC, the rotating column is driven to rotate through the output shaft of the first servo motor, the storage box is driven to rotate through the rotating column, the weighing sensor is enabled to rotate 180 ℃ under the action of the second positioning block, raw materials in the storage box can be poured out, the first positioning block plays a role in positioning, and the annular material guiding block plays a role in guiding materials;|(4) Starting a second servo motor to operate through a PLC (programmable logic controller), enabling the second servo motor to drive a first auger to rotate through an output shaft of the second servo motor, enabling unqualified broken materials to drop into a shell through a first port, enabling the first auger to operate the materials, enabling the second servo motor to discharge the materials between two breaking rollers again through the cooperation of the second port and a material guide plate, and enabling the two breaking rollers to break the materials again until the materials are qualified;|s3, acid treatment:|(1) Opening a second electromagnetic valve on a discharging pipe through a PLC (programmable logic controller) to enable the weighed materials to be discharged into a box body through the discharging pipe, then opening a sealing cover on the charging pipe to enable the sealing cover to be added into the box body through the charging pipe, then starting a third servo motor to operate through the PLC to enable the third servo motor to drive a second bevel gear to rotate through an output shaft of the PLC to enable the second bevel gear and the first connecting pipe to rotate under the meshed effect, enabling the first bevel gear, the second connecting pipe, the second hollow plate and the heating pipe to rotate through the first connecting pipe, mixing, heating and stirring raw materials in the box body, supplying power to the heating wire to enable the heating wire to generate heat, further heating the raw materials in the box body, opening a fifth electromagnetic valve on the discharging pipe through the PLC to enable the heating pipe to emit brown gas, continuously heating the solution to be changed from black to green, enabling the solution to be changed from light green to milky yellow when the temperature is raised to 250 ℃, and enabling the brown gas to disappear, indicating that the reaction carbon is removed, and the reaction time is 30min;|(2) If the solution does not change into cream yellow, continuously heating to 280 ℃ to release a large amount of white smoke, stopping heating, cooling to 200 ℃ to slowly dropwise add nitric acid to release a large amount of reddish brown gas, quickly disappearing, adding a proper amount of nitric acid until the brown gas does not disappear any more, heating until the solution becomes cream yellow, and repeatedly operating until the solution changes color if the solution does not change color;|(3) After the reaction, cooling to room temperature, then opening the third solenoid valve for raw materials in the box enter into the transportation pipe through the feed opening, then start driving motor and operate, drive the second auger through driving motor's output shaft and rotate, make it operate the raw materials through the second auger, cause the raw materials to discharge the rose box in, then fall to the second filter on the filter and filter, and the acid water can fall to the below of second filter and fall to the bottom inner wall of rose box, and the material on the second filter then can be discharged through the discharge gate, make it drop to the transportation equipment on transport. (CN114735664)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of production of cubic boron nitride, and particularly relates to an automatic acid washing device and method for production of cubic boron nitride.|BACKGROUND ART|[0002] The invention discloses an automatic acid washing device for producing cubic boron nitride, which comprises an acid washing barrel, wherein a stirring mechanism is arranged in the acid washing barrel, a plastic filter barrel is arranged above the stirring mechanism, a support column is vertically arranged at the right end in the acid washing barrel, the upper end of the support column is hinged with the right end of the plastic filter barrel, a lifting mechanism is arranged at the upper end of the acid washing barrel, a plastic rope connected with the left end of the plastic filter barrel is arranged at the upper end of the plastic filter barrel, a first water inlet pipe is arranged at the upper end of the plastic filter barrel, a discharging funnel is coaxially arranged at the right end of the plastic filter barrel, the first water inlet pipe is arranged at the upper end of the plastic filter barrel, an automatic acid washing device for producing cubic boron nitride is arranged at the upper end of the plastic filter barrel, a first water outlet pipe is arranged at the upper end of the lower end of the plastic filter barrel, and an automatic acid washing pipe is arranged at the lower end of the plastic filter barrel.|[0003] However, the structure has the defects that the strong oxidant perchloric acid is generally adopted to heat and concentrate for removing carbon when acid washing and carbon removal are carried out on opposite boron nitride at present, but perchloric acid is a flammable and explosive substance, so that the operation is extremely unsafe and is easy to cause harm to the body of staff.|[0004] Therefore, there is a need to provide a new automatic acid cleaning device and method for cubic boron nitride production, which solve the above technical problems.|DISCLOSURE|Disclosure of Invention|[0005] The invention solves the technical problem of providing an automatic acid washing device and an automatic acid washing method for producing cubic boron nitride, which can strengthen the acid washing and carbon removing effects, so that the safety purification of cubic boron nitride can be carried out while the harm to the body of staff can be avoided.|[0006] In order to solve the technical problems, the automatic acid washing device and method for producing cubic boron nitride provided by the invention comprise the following steps: the device comprises a box body, a processing box, a filtering box and a crushing weighing mechanism, wherein the processing box is arranged on the top of the box body, the filtering box is arranged on the outer wall of one side of the box body, and the crushing weighing mechanism is arranged on the processing box;|[0007] the crushing weighing mechanism comprises two rotating rods, two crushing rollers, a connecting motor, a first filter plate, a rotating column, a first servo motor, a funnel, a storage box, a weighing sensor, a placing plate and a circulating assembly, wherein the two rotating rods are rotatably installed in the treatment box, one end of each corresponding rotating rod extends out of one side of the treatment box, the two crushing rollers are arranged in the treatment box, the two crushing rollers are fixedly installed on the two rotating rods respectively, the two crushing rollers are meshed, the connecting motor is fixedly installed on one side outer wall of the treatment box, an output shaft of the connecting motor is fixedly connected with one end of each corresponding rotating rod, the first filter plate is arranged in the treatment box, the rotating column is rotatably installed in the treatment box, the rotating column is positioned below the first filter plate, one side of the rotating column extends out of one side of the treatment box, the first servo motor is fixedly installed on one side outer wall of the treatment box, an output shaft of the first servo motor is fixedly connected with one side outer wall of the rotating column, the funnel is arranged in the treatment box, the first filter plate is fixedly connected with one side outer wall of the corresponding rotating column, the weighing sensor is fixedly connected with the first filter plate, the weighing sensor is arranged on the bottom of the storage box, the weighing sensor is fixedly arranged on the top of the storage box, and the weighing sensor is fixedly arranged on the top of the storage box;|[0008] the circulating assembly is arranged on the treatment box;|[0009] the heating device comprises a box body, and is characterized in that a stirring heating mechanism is arranged on the box body and comprises a first connecting pipe, a first conical gear, a third servo motor, a second conical gear, a first hollow plate, a second connecting pipe, a second hollow plate, four heating pipes, a heating layer and heating wires, wherein the first connecting pipe is rotatably arranged on the inner wall of the top of the box body, the top end of the first connecting pipe extends to the upper part of the top of the box body, the first conical gear is fixedly sleeved on the first connecting pipe, the first conical gear is positioned above the top of the box body, the third servo motor is fixedly arranged on the top of the box body, the second conical gear is fixedly arranged on an output shaft of the third servo motor, the second conical gear is meshed with the first conical gear, the first hollow plate is arranged in the box body, the first hollow plate is fixedly arranged on the bottom end of the first connecting pipe, the second connecting pipe is fixedly arranged on the bottom of the first hollow plate, the second hollow plate is fixedly arranged on the bottom of the second hollow plate, the fourth heating pipe is fixedly arranged on the bottom of the fourth heating pipe, and the heating wire is arranged in the hollow heating layer.|[0010] As a further scheme of the invention, the circulating assembly comprises a shell, a second servo motor, a first auger and a material guiding plate, wherein the shell is fixedly arranged on the outer wall of one side of the treatment box, the second servo motor is fixedly arranged on the top of the shell, the first auger is rotatably arranged in the shell, the top end of the first auger extends to the upper part of the top of the shell and is fixedly connected with the output shaft of the second servo motor, and the material guiding plate is fixedly arranged in the treatment box.|[0011] As a further scheme of the invention, a first through hole is formed in the inner wall of one side of the treatment box, the first through hole is communicated with the shell, the first through hole is matched with the first filter plate, a second through hole is formed in the inner wall of one side of the treatment box, the second through hole is communicated with the shell, and the second through hole is matched with the material guide plate.|[0012] As a further scheme of the invention, a positioning assembly is arranged on the treatment box and comprises a first positioning block, an annular guide block and a second positioning block, wherein the first positioning block is arranged in the treatment box, the first positioning block is positioned behind the storage box and is matched with the storage box, the annular guide block is arranged on the inner wall of the bottom of the treatment box and is matched with the storage box, the second positioning block is arranged on the annular guide block and is positioned below the first positioning block, the second positioning block is matched with the storage box, a discharge pipe is fixedly arranged at the bottom of the treatment box, a second electromagnetic valve is arranged on the discharge pipe, and the bottom end of the discharge pipe extends into the box.|[0013] As a further scheme of the invention, the box body is provided with a transportation assembly, the transportation assembly comprises a transportation pipe, a driving motor, a baffle plate and a second auger, the transportation pipe is arranged in the box body, the driving motor is fixedly arranged in the transportation pipe, the baffle plate is fixedly arranged in the transportation pipe, the second auger is arranged in the transportation pipe, penetrates through the baffle plate and is rotationally connected with the baffle plate, one end of the second auger is fixedly connected with an output shaft of the driving motor, and one end of the second auger, which is far away from the baffle plate, extends into the filter box.|[0014] As a further scheme of the invention, a discharging opening is formed in the box body and is communicated with the conveying pipe, a third electromagnetic valve is arranged on the discharging opening, a third port is formed in the outer wall of one side of the filter box and is communicated with the conveying pipe, and the third port is matched with the second auger.|[0015] As a further scheme of the invention, a second filter plate is arranged in the filter box and is positioned below the second auger, a discharge hole is formed in the outer wall of one side of the filter box, a conveying device is arranged below the bottom of the filter box, a liquid discharge pipe is fixedly arranged at the bottom of the filter box, a fourth electromagnetic valve is arranged on the liquid discharge pipe, a material baffle is arranged on the outer wall of one side of the filter box, and the material baffle is matched with the discharge hole.|[0016] As a further scheme of the invention, a feed hopper is arranged at the top of the treatment box, a feed pipe is arranged at the top of the box body, a sealing cover is arranged on the feed pipe, an exhaust pipe is arranged on the outer wall of one side of the box body, a fifth electromagnetic valve is arranged on the exhaust pipe, a temperature sensor is arranged on the inner wall of the top of the box body, a PLC (programmable logic controller) is arranged on the outer wall of one side of the box body, and an observation window is arranged on the box body.|[0017] The invention also provides an automatic acid washing method for producing the cubic boron nitride, which comprises the following steps of:|[0018] s1, raw materials:|[0019] (1) Cubic boron nitride, mixed acid;|[0020] s2, crushing and screening:|[0021] (1) Starting a connecting motor to operate through a PLC (programmable logic controller), driving a rotating rod to rotate through an output shaft of the connecting motor, driving crushing rollers to rotate through the rotating rod, enabling two crushing rollers to mutually approach to each other to rotate under the meshing effect, and then throwing cubic boron nitride into a processing box through a feed hopper on the processing box to enable the cubic boron nitride to fall onto the two crushing rollers, so that the cubic boron nitride is crushed oppositely through the two crushing rollers;|[0022] (2) Broken material can enter into the funnel through first filter, and first filter then plays the effect of screening, first filter is the mesh, then opens the first solenoid valve on the funnel through the PLC controller, cause the material that filters to enter into the bin through the funnel, make it drop place on the board, and along with placing the material on the board more and more, consequently, can extrude weighing sensor under the effect of gravity, thereby weigh through weighing sensor, and show on passing the result to the PLC controller, cause convenient staff to control it, when the material reaches, then can close first solenoid through the PLC controller:|[0023] (3) The first servo motor is started to operate through the PLC, the rotating column is driven to rotate through the output shaft of the first servo motor, the storage box is driven to rotate through the rotating column, the weighing sensor is enabled to rotate 180 ℃ under the action of the second positioning block, raw materials in the storage box can be poured out, the first positioning block plays a role in positioning, and the annular material guiding block plays a role in guiding materials;|[0024] (4) Starting a second servo motor to operate through a PLC (programmable logic controller), enabling the second servo motor to drive a first auger to rotate through an output shaft of the second servo motor, enabling unqualified broken materials to drop into a shell through a first port, enabling the first auger to operate the materials, enabling the second servo motor to discharge the materials between two breaking rollers again through the cooperation of the second port and a material guide plate, and enabling the two breaking rollers to break the materials again until the materials are qualified;|[0025] s3, acid treatment:|[0026] (1) Opening a second electromagnetic valve on a discharging pipe through a PLC (programmable logic controller) to enable the weighed materials to be discharged into a box body through the discharging pipe, then opening a sealing cover on the charging pipe to enable the sealing cover to be added into the box body through the charging pipe, then starting a third servo motor to operate through the PLC to enable the third servo motor to drive a second bevel gear to rotate through an output shaft of the PLC to enable the second bevel gear and the first connecting pipe to rotate under the meshed effect, enabling the first hollow plate, the second connecting pipe, the second hollow plate and the heating pipe to rotate through the first connecting pipe, mixing, heating and stirring raw materials in the box body, supplying power to the heating wire to enable the heating wire to generate heat, further heating the raw materials in the box body, opening a fifth electromagnetic valve on the discharging pipe through the PLC to enable the heating pipe to emit brown gas, continuously heating the solution to be changed from black to green, enabling the solution to be changed from light green to milky yellow when the temperature is raised to 250 ℃, and enabling the brown gas to disappear, indicating that the reaction carbon is removed, and the reaction time is 30min;|[0027] (2) If the solution does not change into cream yellow, continuously heating to 280 ℃ to release a large amount of white smoke, stopping heating, cooling to 200 ℃ to slowly dropwise add nitric acid to release a large amount of reddish brown gas, quickly disappearing, adding a proper amount of nitric acid until the brown gas does not disappear any more, heating until the solution becomes cream yellow, and repeatedly operating until the solution changes color if the solution does not change color;|[0028] (3) After the reaction, cooling to room temperature, then opening the third solenoid valve for raw materials in the box enter into the transportation pipe through the feed opening, then start driving motor and operate, drive the second auger through driving motor's output shaft and rotate, make it operate the raw materials through the second auger, cause the raw materials to discharge the rose box in, then fall to the second filter on the filter and filter, and the acid water can fall to the below of second filter and fall to the bottom inner wall of rose box, and the material on the second filter then can be discharged through the discharge gate, make it drop to the transportation equipment on transport.|[0029] Compared with the related art, the automatic acid washing device and method for producing the cubic boron nitride have the following beneficial effects:|[0030] 1. according to the invention, the graphite, the sulfuric acid and the nitric acid do not react at high temperature (the cubic boron nitride has good stability), and the graphite, the sulfuric acid and the nitric acid can react to generate carbon dioxide gas and substances which are easy to dissolve in water, so that the aim of removing carbon can be fulfilled, and further safety purification can be realized by opposite nitriding, and meanwhile, the harm to the body of staff can be avoided.|[0031] 2. Because cubic boron nitride has good stability, the cubic boron nitride does not react with sulfuric acid and nitric acid at high temperature, and graphite reacts with sulfuric acid and nitric acid to generate carbon dioxide gas and substances which are easy to dissolve in water, thereby achieving the purpose of removing carbon.|DRAWINGS DESCRIPTION|[0032] The present invention is further described below with reference to the accompanying drawings for the convenience of understanding by those skilled in the art.|[0033] FIG. 1 is a front view of the present invention;|[0034] FIG. 2 is a schematic elevational view of the present invention;|[0035] FIG. 3 is a schematic view of the structure of the treatment tank of the present invention;|[0036] FIG. 4 is an enlarged schematic view of the portion A in FIG. 2;|[0037] fig. 5 is an enlarged schematic view of the portion B in fig. 2.|[0038] In the figure: 1. a case; 2. a treatment box; 3. a filter box; 4. a rotating rod; 5. a crushing roller; 6. a first filter plate; 7. rotating the column; 8. a first servo motor; 9. a funnel; 10. a storage tank; 11. a weighing sensor; 12. placing a plate; 13. a housing; 14. a second servo motor; 15. a first auger; 16. a material guide plate; 17. a discharge pipe; 18. a first connection pipe; 19. a first bevel gear; 20. a third servo motor; 21. a second bevel gear; 22. a first hollow slab; 23. a second connection pipe; 24. a second hollow slab; 25. heating pipes; 26. a heating layer; 27. heating wires; 28. a transport tube; 29. a driving motor; 30. a baffle; 31. a second auger; 32. a second filter plate; 33. a transport device; 34. a temperature sensor; 35. and a PLC controller.|INVENTION MODE|Detailed Description|[0039] Referring to fig. 1, fig. 2, fig. 3, fig. 4, and fig. 5, in which fig. 1 is a front view of the present invention; FIG. 2 is a schematic elevational view of the present invention; FIG. 3 is a schematic view of the structure of the treatment tank of the present invention; FIG. 4 is an enlarged schematic view of the portion A in FIG. 2; fig. 5 is an enlarged schematic view of the portion B in fig. 2. An automatic acid washing device for cubic boron nitride production comprises: the device comprises a box body 1, a processing box 2, a filtering box 3 and a crushing weighing mechanism, wherein the processing box 2 is arranged on the top of the box body 1, the filtering box 3 is arranged on the outer wall of one side of the box body 1, and the crushing weighing mechanism is arranged on the processing box 2;|[0040] the crushing weighing mechanism comprises two rotating rods 4, two crushing rollers 5, a connecting motor, a first filter plate 6, a rotating column 7, a first servo motor 8, a funnel 9, a storage box 10, a weighing sensor 11, a placing plate 12 and a circulating assembly, wherein the two rotating rods 4 are rotatably installed in the processing box 2, one end of the corresponding rotating rod 4 extends out of one side of the processing box 2, the two crushing rollers 5 are fixedly installed in the processing box 2, the two crushing rollers 5 are fixedly installed on the two rotating rods 4 respectively, the two crushing rollers 5 are meshed, the connecting motor is fixedly installed on the outer wall of one side of the processing box 2, an output shaft of the connecting motor is fixedly connected with one end of the corresponding rotating rod 4, the first filter plate 6 is arranged in the processing box 2, the rotating column 7 is rotatably installed in the processing box 2, the rotating column 7 is positioned below the first filter plate 6, one side of the rotating column 7 extends out of one side of the processing box 2, the first servo motor 8 is fixedly installed on the outer wall of one side of the processing box 2, the first filter plate 8 is fixedly installed on the outer wall of the first servo motor, the first filter plate 8 is fixedly installed on the first filter plate 8 and the first filter plate 10 is fixedly installed on the bottom of the storage box 10, the first filter plate 10 is fixedly installed on the bottom part 10, and is fixedly installed on the first filter plate 10, and is fixedly installed on the bottom filter plate 10 and is arranged on the bottom 10 and is fixedly placed on the bottom 10 filter 10;|[0041] the circulating assembly is arranged on the treatment box 2;|[0042] the stirring and heating mechanism is arranged on the box body 1 and comprises a first connecting pipe 18, a first conical gear 19, a third servo motor 20, a second conical gear 21, a first hollow plate 22, a second connecting pipe 23, a second hollow plate 24, four heating pipes 25, a heating layer 26 and heating wires 27, wherein the first connecting pipe 18 is rotatably arranged on the inner wall of the top of the box body 1, the top end of the first connecting pipe 18 extends to the top of the box body 1, the first conical gear 19 is fixedly sleeved on the first connecting pipe 18, the first conical gear 19 is positioned on the top of the box body 1, the third servo motor 20 is fixedly arranged on the top of the box body 1, the second conical gear 21 is fixedly arranged on the output shaft of the third servo motor 20, the second conical gear 21 is meshed with the first conical gear 19, the first hollow plate 22 is arranged in the box body 1, the bottom end of the first connecting pipe 18 is fixedly arranged on the bottom of the first connecting pipe 18, the second conical gear 19 is fixedly arranged on the second hollow plate 24 and the fourth hollow plate 25, the heating wires 25 are fixedly arranged on the bottom of the fourth hollow plate 24 and the fourth hollow plate 25, and the fourth hollow plate 25 is fixedly arranged on the bottom of the fourth connecting pipe 24.|[0043] The circulating assembly comprises a shell 13, a second servo motor 14, a first auger 15 and a material guide plate 16, wherein the shell 13 is fixedly arranged on the outer wall of one side of the treatment box 2, the second servo motor 14 is fixedly arranged on the top of the shell 13, the first auger 15 is rotatably arranged in the shell 13, the top end of the first auger 15 extends to the upper part of the top of the shell 13 and is fixedly connected with the output shaft of the second servo motor 14, and the material guide plate 16 is fixedly arranged in the treatment box 2.|[0044] The first through hole is formed in the inner wall of one side of the processing box 2 and is communicated with the shell 13, the first through hole is matched with the first filter plate 6, the second through hole is formed in the inner wall of one side of the processing box 2 and is communicated with the shell 13, and the second through hole is matched with the guide plate 16.|[0045] The processing box 2 is provided with a positioning assembly, the positioning assembly comprises a first positioning block, an annular guide block and a second positioning block, the first positioning block is arranged in the processing box 2, the first positioning block is positioned at the rear of the storage box 10 and is matched with the storage box 10, the annular guide block is arranged on the inner wall of the bottom of the processing box 2, the annular guide block is matched with the storage box 10, the second positioning block is arranged on the annular guide block, the second positioning block is positioned below the first positioning block, the second positioning block is matched with the storage box 10, a discharge pipe 17 is fixedly arranged at the bottom of the processing box 2, a second electromagnetic valve is arranged on the discharge pipe 17, and the bottom end of the discharge pipe 17 extends into the box 1.|[0046] Be equipped with transport assembly on the box 1, transport assembly is including transport pipe 28, driving motor 29, baffle 30 and second auger 31, transport pipe 28 is seted up in box 1, driving motor 29 fixed mounting is in transport pipe 28, baffle 30 fixed mounting is in transport pipe 28, second auger 31 sets up in transport pipe 28, second auger 31 runs through baffle 30 and rotates with baffle 30 to be connected, the one end of second auger 31 and driving motor 29's output shaft fixed connection, the one end that baffle 30 was kept away from to second auger 31 extends to in the rose box 3.|[0047] The box body 1 is provided with a discharging opening, the discharging opening is communicated with the conveying pipe 28, the discharging opening is provided with a third electromagnetic valve, the outer wall of one side of the filter box 3 is provided with a third opening, the third opening is communicated with the conveying pipe 28, and the third opening is matched with the second auger 31.|[0048] Be equipped with second filter 32 in the rose box 3, second filter 32 is located the below of second auger 31, the discharge gate has been seted up to one side outer wall of rose box 3, the bottom below of rose box 3 is equipped with transportation equipment 33, the bottom fixed mounting of rose box 3 has the fluid-discharge tube, be equipped with the fourth solenoid valve on the fluid-discharge tube, one side outer wall of rose box 3 is equipped with the striker plate, striker plate and discharge gate looks adaptation.|[0049] The top of handling case 2 is equipped with the feeder hopper, the top of box 1 is equipped with the filling tube, be equipped with sealed lid on the filling tube, one side outer wall of box 1 is equipped with the blast pipe, be equipped with the fifth solenoid valve on the blast pipe, the top inner wall of box 1 is equipped with temperature sensor 34, one side outer wall of box 1 is equipped with PLC controller 35, be equipped with the observation window on the box 1.|[0050] In addition, the invention also provides an automatic acid washing method for producing the cubic boron nitride.|[0051] Comprises the following raw materials and a box body 1:|[0052] s1, raw materials:|[0053] (1) Cubic boron nitride, mixed acid;|[0054] s2, crushing and screening:|[0055] (1) Starting a connecting motor to operate through a PLC (programmable logic controller) 35, driving a rotating rod 4 to rotate through an output shaft of the connecting motor, driving a crushing roller 5 to rotate through the rotating rod 4, enabling the two crushing rollers 5 to mutually approach to each other to rotate under the meshing action, and then throwing cubic boron nitride into the processing box 2 through a feed hopper on the processing box 2, so that the cubic boron nitride falls onto the two crushing rollers 5, and crushing the cubic boron nitride oppositely through the two crushing rollers 5;|[0056] (2) Broken materials can enter the hopper 9 through the first filter plate 6, the first filter plate 6 plays a screening role, the first filter plate 6 is 46 meshes, then a first electromagnetic valve on the hopper 9 is opened through the PLC 35, the screened materials enter the storage box 10 through the hopper 9 and fall onto the placing plate 12, and the weighing sensor 11 is extruded along with the more and more materials on the placing plate 12 under the action of gravity, so that the weighing sensor 11 is used for weighing, the result is transmitted to the PLC 35 for display (the ratio of the materials to mixed acid (sulfuric acid and nitric acid) is 1:10-20), so that the materials are convenient for workers to handle and control, and when the materials reach, the first electromagnetic valve can be closed through the PLC 35:|[0057] (3) The first servo motor 8 is started to operate through the PLC 35, the rotating column 7 is driven to rotate through the output shaft of the first servo motor 8, the storage box 10 is driven to rotate through the rotating column 7, the weighing sensor 11 is rotated by 180 ℃ under the action of the second positioning block, raw materials in the storage box 10 can be poured out, the first positioning block plays a role in positioning, and the annular material guiding block plays a role in guiding materials;|[0058] (4) The second servo motor 14 is started to operate through the PLC 35, the first auger 15 is driven to rotate through the output shaft of the second servo motor 14, and the unqualified materials are dropped into the shell 13 through the first through hole, so that the materials can be operated under the action of the first auger 15, and then the materials can be discharged between the two crushing rollers 5 again through the cooperation of the second through hole and the material guide plate 16, and then the materials are crushed again through the two crushing rollers 5 until the materials are qualified;|[0059] s3, acid treatment:|[0060] (1) Opening a second electromagnetic valve on the discharge pipe 17 through the PLC 35 to enable the weighed materials to be discharged into the box body 1 through the discharge pipe 17, then opening a sealing cover on the feed pipe to enable the materials to be added into the box body 1 through the feed pipe, then starting a third servo motor 20 through the PLC 35 to operate, enabling the materials to drive a second bevel gear 21 to rotate through an output shaft of the PLC 35 to enable the materials to drive a first bevel gear 19 and a first connecting pipe 18 to rotate under the meshing effect, enabling the first hollow plate 22, the second connecting pipe 23, the second hollow plate 24 and the heating pipe 25 to rotate through the first connecting pipe 18, carrying out mixed heating stirring on the materials in the box body 1, and enabling the heating wire 27 to generate heat through supplying power to the heating wire 27, further heating the materials in the box body 1, opening a fifth electromagnetic valve on the exhaust pipe through the PLC 35 to enable the exhaust pipe to be heated to release gas, continuously heating, enabling the solution to change from black to light green (through an observation window), enabling the temperature to rise to 250 ℃ to change from light brown to light brown, and showing that the light brown black to light brown, and the light brown carbon is removed, and the clear black carbon is completely removed, and the brown carbon is a clear, and the brown carbon solution is completely removed, and the brown reaction is shown by 30;|[0061] (2) If the solution does not change into cream yellow, continuously heating to 280 ℃ to release a large amount of white smoke, stopping heating, cooling to 200 ℃ to slowly dropwise add nitric acid to release a large amount of reddish brown gas, quickly disappearing, adding a proper amount of nitric acid until the brown gas does not disappear any more, heating until the solution becomes cream yellow, and repeatedly operating until the solution changes color if the solution does not change color;|[0062] (3) After the reaction, cooling to room temperature, then opening the third electromagnetic valve, enabling the raw materials in the box body 1 to enter the conveying pipe 28 through the discharging opening, then starting the driving motor 29 to operate, driving the second auger 31 to rotate through the output shaft of the driving motor 29, enabling the second auger 31 to operate the raw materials, enabling the raw materials to be discharged into the filter box 3, then falling onto the second filter plate 32 for filtering, enabling acid water to fall onto the lower portion of the second filter plate 32 and fall onto the inner wall of the bottom of the filter box 3, and enabling materials on the second filter plate 32 to be discharged through the discharging opening and to fall onto the conveying equipment 33 for conveying.|[0063] The PLC controller 35 is connected with the connecting motor, the first servo motor 8, the weighing sensor 11, the second servo motor 14, the third servo motor 20, the driving motor 29 and the temperature sensor 34; the PLC controller 35 is connected to the first, second, third, fourth, and fifth solenoid valves.|[0064] It should be noted that, the device structure and the drawings of the present invention mainly describe the principle of the present invention, in terms of the technology of the design principle, the arrangement of the power mechanism, the power supply system, the control system, etc. of the device is not completely described, and on the premise that the person skilled in the art understands the principle of the present invention, the specific details of the power mechanism, the power supply system and the control system can be clearly known, the control mode of the application file is automatically controlled by the controller, and the control circuit of the controller can be realized by simple programming of the person skilled in the art;|[0065] the standard parts used in the method can be purchased from the market, and can be customized according to the description of the specification and the drawings, the specific connection modes of the parts are conventional means such as mature bolts, rivets and welding in the prior art, the machines, the parts and the equipment are conventional models in the prior art, and the structures and the principles of the parts are all known by the skilled person through technical manuals or through conventional experimental methods.|[0066] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations may be made therein without departing from the spirit and scope of the invention as defined by the appended claims and their equivalents, and in other related technical fields, which are equally encompassed by the scope of the present invention. (CN114735664)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of production of cubic boron nitride, and particularly relates to an automatic acid washing device and method for production of cubic boron nitride.|BACKGROUND ART|[0002] The invention discloses an automatic acid washing device for producing cubic boron nitride, which comprises an acid washing barrel, wherein a stirring mechanism is arranged in the acid washing barrel, a plastic filter barrel is arranged above the stirring mechanism, a support column is vertically arranged at the right end in the acid washing barrel, the upper end of the support column is hinged with the right end of the plastic filter barrel, a lifting mechanism is arranged at the upper end of the acid washing barrel, a plastic rope connected with the left end of the plastic filter barrel is arranged at the upper end of the plastic filter barrel, a first water inlet pipe is arranged at the upper end of the plastic filter barrel, a discharging funnel is coaxially arranged at the right end of the plastic filter barrel, the first water inlet pipe is arranged at the upper end of the plastic filter barrel, an automatic acid washing device for producing cubic boron nitride is arranged at the upper end of the plastic filter barrel, a first water outlet pipe is arranged at the upper end of the lower end of the plastic filter barrel, and an automatic acid washing pipe is arranged at the lower end of the plastic filter barrel.|[0003] However, the structure has the defects that the strong oxidant perchloric acid is generally adopted to heat and concentrate for removing carbon when acid washing and carbon removal are carried out on opposite boron nitride at present, but perchloric acid is a flammable and explosive substance, so that the operation is extremely unsafe and is easy to cause harm to the body of staff.|[0004] Therefore, there is a need to provide a new automatic acid cleaning device and method for cubic boron nitride production, which solve the above technical problems.|DISCLOSURE|Disclosure of Invention|[0005] The invention solves the technical problem of providing an automatic acid washing device and an automatic acid washing method for producing cubic boron nitride, which can strengthen the acid washing and carbon removing effects, so that the safety purification of cubic boron nitride can be carried out while the harm to the body of staff can be avoided.|[0006] In order to solve the technical problems, the automatic acid washing device and method for producing cubic boron nitride provided by the invention comprise the following steps: the device comprises a box body, a processing box, a filtering box and a crushing weighing mechanism, wherein the processing box is arranged on the top of the box body, the filtering box is arranged on the outer wall of one side of the box body, and the crushing weighing mechanism is arranged on the processing box;|[0007] the crushing weighing mechanism comprises two rotating rods, two crushing rollers, a connecting motor, a first filter plate, a rotating column, a first servo motor, a funnel, a storage box, a weighing sensor, a placing plate and a circulating assembly, wherein the two rotating rods are rotatably installed in the treatment box, one end of each corresponding rotating rod extends out of one side of the treatment box, the two crushing rollers are arranged in the treatment box, the two crushing rollers are fixedly installed on the two rotating rods respectively, the two crushing rollers are meshed, the connecting motor is fixedly installed on one side outer wall of the treatment box, an output shaft of the connecting motor is fixedly connected with one end of each corresponding rotating rod, the first filter plate is arranged in the treatment box, the rotating column is rotatably installed in the treatment box, the rotating column is positioned below the first filter plate, one side of the rotating column extends out of one side of the treatment box, the first servo motor is fixedly installed on one side outer wall of the treatment box, an output shaft of the first servo motor is fixedly connected with one side outer wall of the rotating column, the funnel is arranged in the treatment box, the first filter plate is fixedly connected with one side outer wall of the corresponding rotating column, the weighing sensor is fixedly connected with the first filter plate, the weighing sensor is arranged on the bottom of the storage box, the weighing sensor is fixedly arranged on the top of the storage box, and the weighing sensor is fixedly arranged on the top of the storage box;|[0008] the circulating assembly is arranged on the treatment box;|[0009] the heating device comprises a box body, and is characterized in that a stirring heating mechanism is arranged on the box body and comprises a first connecting pipe, a first conical gear, a third servo motor, a second conical gear, a first hollow plate, a second connecting pipe, a second hollow plate, four heating pipes, a heating layer and heating wires, wherein the first connecting pipe is rotatably arranged on the inner wall of the top of the box body, the top end of the first connecting pipe extends to the upper part of the top of the box body, the first conical gear is fixedly sleeved on the first connecting pipe, the first conical gear is positioned above the top of the box body, the third servo motor is fixedly arranged on the top of the box body, the second conical gear is fixedly arranged on an output shaft of the third servo motor, the second conical gear is meshed with the first conical gear, the first hollow plate is arranged in the box body, the first hollow plate is fixedly arranged on the bottom end of the first connecting pipe, the second connecting pipe is fixedly arranged on the bottom of the first hollow plate, the second hollow plate is fixedly arranged on the bottom of the second hollow plate, the fourth heating pipe is fixedly arranged on the bottom of the fourth heating pipe, and the heating wire is arranged in the hollow heating layer.|[0010] As a further scheme of the invention, the circulating assembly comprises a shell, a second servo motor, a first auger and a material guiding plate, wherein the shell is fixedly arranged on the outer wall of one side of the treatment box, the second servo motor is fixedly arranged on the top of the shell, the first auger is rotatably arranged in the shell, the top end of the first auger extends to the upper part of the top of the shell and is fixedly connected with the output shaft of the second servo motor, and the material guiding plate is fixedly arranged in the treatment box.|[0011] As a further scheme of the invention, a first through hole is formed in the inner wall of one side of the treatment box, the first through hole is communicated with the shell, the first through hole is matched with the first filter plate, a second through hole is formed in the inner wall of one side of the treatment box, the second through hole is communicated with the shell, and the second through hole is matched with the material guide plate.|[0012] As a further scheme of the invention, a positioning assembly is arranged on the treatment box and comprises a first positioning block, an annular guide block and a second positioning block, wherein the first positioning block is arranged in the treatment box, the first positioning block is positioned behind the storage box and is matched with the storage box, the annular guide block is arranged on the inner wall of the bottom of the treatment box and is matched with the storage box, the second positioning block is arranged on the annular guide block and is positioned below the first positioning block, the second positioning block is matched with the storage box, a discharge pipe is fixedly arranged at the bottom of the treatment box, a second electromagnetic valve is arranged on the discharge pipe, and the bottom end of the discharge pipe extends into the box.|[0013] As a further scheme of the invention, the box body is provided with a transportation assembly, the transportation assembly comprises a transportation pipe, a driving motor, a baffle plate and a second auger, the transportation pipe is arranged in the box body, the driving motor is fixedly arranged in the transportation pipe, the baffle plate is fixedly arranged in the transportation pipe, the second auger is arranged in the transportation pipe, penetrates through the baffle plate and is rotationally connected with the baffle plate, one end of the second auger is fixedly connected with an output shaft of the driving motor, and one end of the second auger, which is far away from the baffle plate, extends into the filter box.|[0014] As a further scheme of the invention, a discharging opening is formed in the box body and is communicated with the conveying pipe, a third electromagnetic valve is arranged on the discharging opening, a third port is formed in the outer wall of one side of the filter box and is communicated with the conveying pipe, and the third port is matched with the second auger.|[0015] As a further scheme of the invention, a second filter plate is arranged in the filter box and is positioned below the second auger, a discharge hole is formed in the outer wall of one side of the filter box, a conveying device is arranged below the bottom of the filter box, a liquid discharge pipe is fixedly arranged at the bottom of the filter box, a fourth electromagnetic valve is arranged on the liquid discharge pipe, a material baffle is arranged on the outer wall of one side of the filter box, and the material baffle is matched with the discharge hole.|[0016] As a further scheme of the invention, a feed hopper is arranged at the top of the treatment box, a feed pipe is arranged at the top of the box body, a sealing cover is arranged on the feed pipe, an exhaust pipe is arranged on the outer wall of one side of the box body, a fifth electromagnetic valve is arranged on the exhaust pipe, a temperature sensor is arranged on the inner wall of the top of the box body, a PLC (programmable logic controller) is arranged on the outer wall of one side of the box body, and an observation window is arranged on the box body.|[0017] The invention also provides an automatic acid washing method for producing the cubic boron nitride, which comprises the following steps of:|[0018] s1, raw materials:|[0019] (1) Cubic boron nitride, mixed acid;|[0020] s2, crushing and screening:|[0021] (1) Starting a connecting motor to operate through a PLC (programmable logic controller), driving a rotating rod to rotate through an output shaft of the connecting motor, driving crushing rollers to rotate through the rotating rod, enabling two crushing rollers to mutually approach to each other to rotate under the meshing effect, and then throwing cubic boron nitride into a processing box through a feed hopper on the processing box to enable the cubic boron nitride to fall onto the two crushing rollers, so that the cubic boron nitride is crushed oppositely through the two crushing rollers;|[0022] (2) Broken material can enter into the funnel through first filter, and first filter then plays the effect of screening, first filter is the mesh, then opens the first solenoid valve on the funnel through the PLC controller, cause the material that filters to enter into the bin through the funnel, make it drop place on the board, and along with placing the material on the board more and more, consequently, can extrude weighing sensor under the effect of gravity, thereby weigh through weighing sensor, and show on passing the result to the PLC controller, cause convenient staff to control it, when the material reaches, then can close first solenoid through the PLC controller:|[0023] (3) The first servo motor is started to operate through the PLC, the rotating column is driven to rotate through the output shaft of the first servo motor, the storage box is driven to rotate through the rotating column, the weighing sensor is enabled to rotate 180 ℃ under the action of the second positioning block, raw materials in the storage box can be poured out, the first positioning block plays a role in positioning, and the annular material guiding block plays a role in guiding materials;|[0024] (4) Starting a second servo motor to operate through a PLC (programmable logic controller), enabling the second servo motor to drive a first auger to rotate through an output shaft of the second servo motor, enabling unqualified broken materials to drop into a shell through a first port, enabling the first auger to operate the materials, enabling the second servo motor to discharge the materials between two breaking rollers again through the cooperation of the second port and a material guide plate, and enabling the two breaking rollers to break the materials again until the materials are qualified;|[0025] s3, acid treatment:|[0026] (1) Opening a second electromagnetic valve on a discharging pipe through a PLC (programmable logic controller) to enable the weighed materials to be discharged into a box body through the discharging pipe, then opening a sealing cover on the charging pipe to enable the sealing cover to be added into the box body through the charging pipe, then starting a third servo motor to operate through the PLC to enable the third servo motor to drive a second bevel gear to rotate through an output shaft of the PLC to enable the second bevel gear and the first connecting pipe to rotate under the meshed effect, enabling the first hollow plate, the second connecting pipe, the second hollow plate and the heating pipe to rotate through the first connecting pipe, mixing, heating and stirring raw materials in the box body, supplying power to the heating wire to enable the heating wire to generate heat, further heating the raw materials in the box body, opening a fifth electromagnetic valve on the discharging pipe through the PLC to enable the heating pipe to emit brown gas, continuously heating the solution to be changed from black to green, enabling the solution to be changed from light green to milky yellow when the temperature is raised to 250 ℃, and enabling the brown gas to disappear, indicating that the reaction carbon is removed, and the reaction time is 30min;|[0027] (2) If the solution does not change into cream yellow, continuously heating to 280 ℃ to release a large amount of white smoke, stopping heating, cooling to 200 ℃ to slowly dropwise add nitric acid to release a large amount of reddish brown gas, quickly disappearing, adding a proper amount of nitric acid until the brown gas does not disappear any more, heating until the solution becomes cream yellow, and repeatedly operating until the solution changes color if the solution does not change color;|[0028] (3) After the reaction, cooling to room temperature, then opening the third solenoid valve for raw materials in the box enter into the transportation pipe through the feed opening, then start driving motor and operate, drive the second auger through driving motor's output shaft and rotate, make it operate the raw materials through the second auger, cause the raw materials to discharge the rose box in, then fall to the second filter on the filter and filter, and the acid water can fall to the below of second filter and fall to the bottom inner wall of rose box, and the material on the second filter then can be discharged through the discharge gate, make it drop to the transportation equipment on transport.|[0029] Compared with the related art, the automatic acid washing device and method for producing the cubic boron nitride have the following beneficial effects:|[0030] 1. according to the invention, the graphite, the sulfuric acid and the nitric acid do not react at high temperature (the cubic boron nitride has good stability), and the graphite, the sulfuric acid and the nitric acid can react to generate carbon dioxide gas and substances which are easy to dissolve in water, so that the aim of removing carbon can be fulfilled, and further safety purification can be realized by opposite nitriding, and meanwhile, the harm to the body of staff can be avoided.|[0031] 2. Because cubic boron nitride has good stability, the cubic boron nitride does not react with sulfuric acid and nitric acid at high temperature, and graphite reacts with sulfuric acid and nitric acid to generate carbon dioxide gas and substances which are easy to dissolve in water, thereby achieving the purpose of removing carbon.|DRAWINGS DESCRIPTION|[0032] The present invention is further described below with reference to the accompanying drawings for the convenience of understanding by those skilled in the art.|[0033] FIG. 1 is a front view of the present invention;|[0034] FIG. 2 is a schematic elevational view of the present invention;|[0035] FIG. 3 is a schematic view of the structure of the treatment tank of the present invention;|[0036] FIG. 4 is an enlarged schematic view of the portion A in FIG. 2;|[0037] fig. 5 is an enlarged schematic view of the portion B in fig. 2.|[0038] In the figure: 1. a case; 2. a treatment box; 3. a filter box; 4. a rotating rod; 5. a crushing roller; 6. a first filter plate; 7. rotating the column; 8. a first servo motor; 9. a funnel; 10. a storage tank; 11. a weighing sensor; 12. placing a plate; 13. a housing; 14. a second servo motor; 15. a first auger; 16. a material guide plate; 17. a discharge pipe; 18. a first connection pipe; 19. a first bevel gear; 20. a third servo motor; 21. a second bevel gear; 22. a first hollow slab; 23. a second connection pipe; 24. a second hollow slab; 25. heating pipes; 26. a heating layer; 27. heating wires; 28. a transport tube; 29. a driving motor; 30. a baffle; 31. a second auger; 32. a second filter plate; 33. a transport device; 34. a temperature sensor; 35. and a PLC controller.|INVENTION MODE|Detailed Description|[0039] Referring to fig. 1, fig. 2, fig. 3, fig. 4, and fig. 5, in which fig. 1 is a front view of the present invention; FIG. 2 is a schematic elevational view of the present invention; FIG. 3 is a schematic view of the structure of the treatment tank of the present invention; FIG. 4 is an enlarged schematic view of the portion A in FIG. 2; fig. 5 is an enlarged schematic view of the portion B in fig. 2. An automatic acid washing device for cubic boron nitride production comprises: the device comprises a box body 1, a processing box 2, a filtering box 3 and a crushing weighing mechanism, wherein the processing box 2 is arranged on the top of the box body 1, the filtering box 3 is arranged on the outer wall of one side of the box body 1, and the crushing weighing mechanism is arranged on the processing box 2;|[0040] the crushing weighing mechanism comprises two rotating rods 4, two crushing rollers 5, a connecting motor, a first filter plate 6, a rotating column 7, a first servo motor 8, a funnel 9, a storage box 10, a weighing sensor 11, a placing plate 12 and a circulating assembly, wherein the two rotating rods 4 are rotatably installed in the processing box 2, one end of the corresponding rotating rod 4 extends out of one side of the processing box 2, the two crushing rollers 5 are fixedly installed in the processing box 2, the two crushing rollers 5 are fixedly installed on the two rotating rods 4 respectively, the two crushing rollers 5 are meshed, the connecting motor is fixedly installed on the outer wall of one side of the processing box 2, an output shaft of the connecting motor is fixedly connected with one end of the corresponding rotating rod 4, the first filter plate 6 is arranged in the processing box 2, the rotating column 7 is rotatably installed in the processing box 2, the rotating column 7 is positioned below the first filter plate 6, one side of the rotating column 7 extends out of one side of the processing box 2, the first servo motor 8 is fixedly installed on the outer wall of one side of the processing box 2, the first filter plate 8 is fixedly installed on the outer wall of the first servo motor, the first filter plate 8 is fixedly installed on the first filter plate 8 and the first filter plate 10 is fixedly installed on the bottom of the storage box 10, the first filter plate 10 is fixedly installed on the bottom part 10, and is fixedly installed on the first filter plate 10, and is fixedly installed on the bottom filter plate 10 and is arranged on the bottom 10 and is fixedly placed on the bottom 10 filter 10;|[0041] the circulating assembly is arranged on the treatment box 2;|[0042] the stirring and heating mechanism is arranged on the box body 1 and comprises a first connecting pipe 18, a first conical gear 19, a third servo motor 20, a second conical gear 21, a first hollow plate 22, a second connecting pipe 23, a second hollow plate 24, four heating pipes 25, a heating layer 26 and heating wires 27, wherein the first connecting pipe 18 is rotatably arranged on the inner wall of the top of the box body 1, the top end of the first connecting pipe 18 extends to the top of the box body 1, the first conical gear 19 is fixedly sleeved on the first connecting pipe 18, the first conical gear 19 is positioned on the top of the box body 1, the third servo motor 20 is fixedly arranged on the top of the box body 1, the second conical gear 21 is fixedly arranged on the output shaft of the third servo motor 20, the second conical gear 21 is meshed with the first conical gear 19, the first hollow plate 22 is arranged in the box body 1, the bottom end of the first connecting pipe 18 is fixedly arranged on the bottom of the first connecting pipe 18, the second conical gear 19 is fixedly arranged on the second hollow plate 24 and the fourth hollow plate 25, the heating wires 25 are fixedly arranged on the bottom of the fourth hollow plate 24 and the fourth hollow plate 25, and the fourth hollow plate 25 is fixedly arranged on the bottom of the fourth connecting pipe 24.|[0043] The circulating assembly comprises a shell 13, a second servo motor 14, a first auger 15 and a material guide plate 16, wherein the shell 13 is fixedly arranged on the outer wall of one side of the treatment box 2, the second servo motor 14 is fixedly arranged on the top of the shell 13, the first auger 15 is rotatably arranged in the shell 13, the top end of the first auger 15 extends to the upper part of the top of the shell 13 and is fixedly connected with the output shaft of the second servo motor 14, and the material guide plate 16 is fixedly arranged in the treatment box 2.|[0044] The first through hole is formed in the inner wall of one side of the processing box 2 and is communicated with the shell 13, the first through hole is matched with the first filter plate 6, the second through hole is formed in the inner wall of one side of the processing box 2 and is communicated with the shell 13, and the second through hole is matched with the guide plate 16.|[0045] The processing box 2 is provided with a positioning assembly, the positioning assembly comprises a first positioning block, an annular guide block and a second positioning block, the first positioning block is arranged in the processing box 2, the first positioning block is positioned at the rear of the storage box 10 and is matched with the storage box 10, the annular guide block is arranged on the inner wall of the bottom of the processing box 2, the annular guide block is matched with the storage box 10, the second positioning block is arranged on the annular guide block, the second positioning block is positioned below the first positioning block, the second positioning block is matched with the storage box 10, a discharge pipe 17 is fixedly arranged at the bottom of the processing box 2, a second electromagnetic valve is arranged on the discharge pipe 17, and the bottom end of the discharge pipe 17 extends into the box 1.|[0046] Be equipped with transport assembly on the box 1, transport assembly is including transport pipe 28, driving motor 29, baffle 30 and second auger 31, transport pipe 28 is seted up in box 1, driving motor 29 fixed mounting is in transport pipe 28, baffle 30 fixed mounting is in transport pipe 28, second auger 31 sets up in transport pipe 28, second auger 31 runs through baffle 30 and rotates with baffle 30 to be connected, the one end of second auger 31 and driving motor 29's output shaft fixed connection, the one end that baffle 30 was kept away from to second auger 31 extends to in the rose box 3.|[0047] The box body 1 is provided with a discharging opening, the discharging opening is communicated with the conveying pipe 28, the discharging opening is provided with a third electromagnetic valve, the outer wall of one side of the filter box 3 is provided with a third opening, the third opening is communicated with the conveying pipe 28, and the third opening is matched with the second auger 31.|[0048] Be equipped with second filter 32 in the rose box 3, second filter 32 is located the below of second auger 31, the discharge gate has been seted up to one side outer wall of rose box 3, the bottom below of rose box 3 is equipped with transportation equipment 33, the bottom fixed mounting of rose box 3 has the fluid-discharge tube, be equipped with the fourth solenoid valve on the fluid-discharge tube, one side outer wall of rose box 3 is equipped with the striker plate, striker plate and discharge gate looks adaptation.|[0049] The top of handling case 2 is equipped with the feeder hopper, the top of box 1 is equipped with the filling tube, be equipped with sealed lid on the filling tube, one side outer wall of box 1 is equipped with the blast pipe, be equipped with the fifth solenoid valve on the blast pipe, the top inner wall of box 1 is equipped with temperature sensor 34, one side outer wall of box 1 is equipped with PLC controller 35, be equipped with the observation window on the box 1.|[0050] In addition, the invention also provides an automatic acid washing method for producing the cubic boron nitride.|[0051] Comprises the following raw materials and a box body 1:|[0052] s1, raw materials:|[0053] (1) Cubic boron nitride, mixed acid;|[0054] s2, crushing and screening:|[0055] (1) Starting a connecting motor to operate through a PLC (programmable logic controller) 35, driving a rotating rod 4 to rotate through an output shaft of the connecting motor, driving a crushing roller 5 to rotate through the rotating rod 4, enabling the two crushing rollers 5 to mutually approach to each other to rotate under the meshing action, and then throwing cubic boron nitride into the processing box 2 through a feed hopper on the processing box 2, so that the cubic boron nitride falls onto the two crushing rollers 5, and crushing the cubic boron nitride oppositely through the two crushing rollers 5;|[0056] (2) Broken materials can enter the hopper 9 through the first filter plate 6, the first filter plate 6 plays a screening role, the first filter plate 6 is 46 meshes, then a first electromagnetic valve on the hopper 9 is opened through the PLC 35, the screened materials enter the storage box 10 through the hopper 9 and fall onto the placing plate 12, and the weighing sensor 11 is extruded along with the more and more materials on the placing plate 12 under the action of gravity, so that the weighing sensor 11 is used for weighing, the result is transmitted to the PLC 35 for display (the ratio of the materials to mixed acid (sulfuric acid and nitric acid) is 1:10-20), so that the materials are convenient for workers to handle and control, and when the materials reach, the first electromagnetic valve can be closed through the PLC 35:|[0057] (3) The first servo motor 8 is started to operate through the PLC 35, the rotating column 7 is driven to rotate through the output shaft of the first servo motor 8, the storage box 10 is driven to rotate through the rotating column 7, the weighing sensor 11 is rotated by 180 ℃ under the action of the second positioning block, raw materials in the storage box 10 can be poured out, the first positioning block plays a role in positioning, and the annular material guiding block plays a role in guiding materials;|[0058] (4) The second servo motor 14 is started to operate through the PLC 35, the first auger 15 is driven to rotate through the output shaft of the second servo motor 14, and the unqualified materials are dropped into the shell 13 through the first through hole, so that the materials can be operated under the action of the first auger 15, and then the materials can be discharged between the two crushing rollers 5 again through the cooperation of the second through hole and the material guide plate 16, and then the materials are crushed again through the two crushing rollers 5 until the materials are qualified;|[0059] s3, acid treatment:|[0060] (1) Opening a second electromagnetic valve on the discharge pipe 17 through the PLC 35 to enable the weighed materials to be discharged into the box body 1 through the discharge pipe 17, then opening a sealing cover on the feed pipe to enable the materials to be added into the box body 1 through the feed pipe, then starting a third servo motor 20 through the PLC 35 to operate, enabling the materials to drive a second bevel gear 21 to rotate through an output shaft of the PLC 35 to enable the materials to drive a first bevel gear 19 and a first connecting pipe 18 to rotate under the meshing effect, enabling the first hollow plate 22, the second connecting pipe 23, the second hollow plate 24 and the heating pipe 25 to rotate through the first connecting pipe 18, carrying out mixed heating stirring on the materials in the box body 1, and enabling the heating wire 27 to generate heat through supplying power to the heating wire 27, further heating the materials in the box body 1, opening a fifth electromagnetic valve on the exhaust pipe through the PLC 35 to enable the exhaust pipe to be heated to release gas, continuously heating, enabling the solution to change from black to light green (through an observation window), enabling the temperature to rise to 250 ℃ to change from light brown to light brown, and showing that the light brown black to light brown, and the light brown carbon is removed, and the clear black carbon is completely removed, and the brown carbon is a clear, and the brown carbon solution is completely removed, and the brown reaction is shown by 30;|[0061] (2) If the solution does not change into cream yellow, continuously heating to 280 ℃ to release a large amount of white smoke, stopping heating, cooling to 200 ℃ to slowly dropwise add nitric acid to release a large amount of reddish brown gas, quickly disappearing, adding a proper amount of nitric acid until the brown gas does not disappear any more, heating until the solution becomes cream yellow, and repeatedly operating until the solution changes color if the solution does not change color;|[0062] (3) After the reaction, cooling to room temperature, then opening the third electromagnetic valve, enabling the raw materials in the box body 1 to enter the conveying pipe 28 through the discharging opening, then starting the driving motor 29 to operate, driving the second auger 31 to rotate through the output shaft of the driving motor 29, enabling the second auger 31 to operate the raw materials, enabling the raw materials to be discharged into the filter box 3, then falling onto the second filter plate 32 for filtering, enabling acid water to fall onto the lower portion of the second filter plate 32 and fall onto the inner wall of the bottom of the filter box 3, and enabling materials on the second filter plate 32 to be discharged through the discharging opening and to fall onto the conveying equipment 33 for conveying.|[0063] The PLC controller 35 is connected with the connecting motor, the first servo motor 8, the weighing sensor 11, the second servo motor 14, the third servo motor 20, the driving motor 29 and the temperature sensor 34; the PLC controller 35 is connected to the first, second, third, fourth, and fifth solenoid valves.|[0064] It should be noted that, the device structure and the drawings of the present invention mainly describe the principle of the present invention, in terms of the technology of the design principle, the arrangement of the power mechanism, the power supply system, the control system, etc. of the device is not completely described, and on the premise that the person skilled in the art understands the principle of the present invention, the specific details of the power mechanism, the power supply system and the control system can be clearly known, the control mode of the application file is automatically controlled by the controller, and the control circuit of the controller can be realized by simple programming of the person skilled in the art;|[0065] the standard parts used in the method can be purchased from the market, and can be customized according to the description of the specification and the drawings, the specific connection modes of the parts are conventional means such as mature bolts, rivets and welding in the prior art, the machines, the parts and the equipment are conventional models in the prior art, and the structures and the principles of the parts are all known by the skilled person through technical manuals or through conventional experimental methods.|[0066] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations may be made therein without departing from the spirit and scope of the invention as defined by the appended claims and their equivalents, and in other related technical fields, which are equally encompassed by the scope of the present invention. Family Number|(100868601)|100868601|Abstract|(CN114735664B B)|The invention provides a novel automatic acid washing device for cubic boron nitride production . The novel automatic acid washing device for cubic boron nitride production comprises a box body , a treatment box , a filter box and a crushing and weighing mechanism , the treatment box is arranged on the top of the box body , the filter box is arranged on the outer wall of one side of the box body , and the crushing and weighing mechanism is arranged on the treatment box ; and the crushing and weighing mechanism comprises two rotating rods , two crushing rollers , a connecting motor , a first filtering plate , a rotating column , a first servo motor , a funnel , a storage box , a weighing sensor , a placing plate and a circulating assembly , and the two rotating rods are rotationally mounted in the treatment box . The novel automatic acid washing device and method for cubic boron nitride production provided by the invention have the advantages that the acid washing and carbon removal effects can be enhanced , so that the harm to the bodies of staff can be avoided while safe purification can be performed on cubic boron nitride . |CPC codes|(CN114735664B B)|B01D - 029/03 |C01B - 021/064/8 |IPC codes|(CN114735664B B)|B01D - 029/03 |C01B - 021/064 | Chemical engineering|Materials, metallurgy B01D-029/03|B02C-004/08|B02C-004/28/6|B02C-023/02|B02C-023/12|C01B-021/064/8|Y02P-020/10 B01D-029/03|B02C-004/08|B02C-004/28/6|B02C-023/02|B02C-023/12|C01B-021/064/8|Y02P-020/10 B01D-029/03|B02C-004/08|B02C-004/28|B02C-023/02|B02C-023/12|C01B-021/064 B01D-029/03|B02C-004/08|B02C-004/28|B02C-023/02|B02C-023/12|C01B-021/064 CN214973969U|GB1262933 CN214973969U 97446560 WHO=Examiner SELF=N|GB1262933 2299213 WHO=Examiner SELF=N CN214973969U; GB1262933 GRANTED (CN114735664)|GRANTED ALIVE (CN114735664)|ALIVE (CN114735664)|LEGAL DETAILS FOR CN114735664|Actual or expected expiration date=2042-03-30|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-03-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210333976|Application date=2022-03-30|Standardized application number=2022CN-0333976|Event publication date=2022-07-12|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114735664|Publication stage code=A|Publication date=2022-07-12|Standardized publication number=CN114735664|Event publication date=2022-07-12|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-07-29|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-05-30|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN114735664|Publication stage code=B|Publication date=2023-05-30|Standardized publication number=CN114735664B|Event publication date=2023-05-30|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN114735664)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTqvxLXjjJ47Bj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067984778&ekey=2107&xpn=CN114735664B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=OWYwMeo85tnhqabKD%252BsTlLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN114735664)|CN|(CN114735664)|CN (CN114735664)|NAME=ZHENGZHOU ZHONGNAN JETE SUPERABRASIVES CO. LTD. , COUNTRY=CN|(CN114735664)|NAME=ZHENGZHOU ZHONGNAN JETE SUPERABRASIVES CO. LTD. , COUNTRY=CN (CN114735664)|NAME=ZHANG LEI;Shenzhen Shenhui Zhicheng Patent Agency (general partnership) , REG=44725|(CN114735664)|NAME=ZHANG LEI;Shenzhen Shenhui Zhicheng Patent Agency (general partnership) , REG=44725 (CN114735664)|NAME=WANG YONGKAI|NAME=ZHANG XIANGFA|NAME=WEI XING|NAME=WANG DAPENG|NAME=LU CUILIAN|NAME=LIU ZHANGJIANG|NAME=ZHANG XIANGXIANG|(CN114735664)|NAME=WANG YONGKAI|NAME=ZHANG XIANGFA|NAME=WEI XING|NAME=WANG DAPENG|NAME=LU CUILIAN|NAME=LIU ZHANGJIANG|NAME=ZHANG XIANGXIANG 0 1 Titre: (CN114735664)|Automatic acid washing device and method for producing cubic boron nitride Résumé: (CN114735664)|The invention provides a novel automatic acid washing device for cubic boron nitride production. The novel automatic acid washing device for cubic boron nitride production comprises a box body, a treatment box, a filter box and a crushing and weighing mechanism, the treatment box is arranged on the top of the box body, the filter box is arranged on the outer wall of one side of the box body, and the crushing and weighing mechanism is arranged on the treatment box; and the crushing and weighing mechanism comprises two rotating rods, two crushing rollers, a connecting motor, a first filtering plate, a rotating column, a first servo motor, a funnel, a storage box, a weighing sensor, a placing plate and a circulating assembly, and the two rotating rods are rotationally mounted in the treatment box. The novel automatic acid washing device and method for cubic boron nitride production provided by the invention have the advantages that the acid washing and carbon removal effects can be enhanced, so that the harm to the bodies of staff can be avoided while safe purification can be performed on cubic boron nitride. 88 Abstract gpt-4o-mini no The article focuses on an automatic acid washing device for cubic boron nitride production, which does not relate to accelerated weathering or CO₂ capture.
89 CN202210223446 CN202210223446 CN114716200|CN114716200 100801613 CN114716200 B 2023-02-03 [CN114716200B]|CN114716200 A 2022-07-08 [CN114716200] 2022-03-07 2022-03-07 2023-02-03|2022-07-08 (CN114716200B)|2023-02-03 (CN114716200)|2042-03-07 (CN114716200)|Carbon capture aggregate using biochar and bottom ash as raw materials and preparation method thereof (CN114716200)|The invention discloses a carbon capture aggregate with biochar and bottom ash as raw materials and a preparation method thereof.The preparation method comprises the steps that waste biomass raw materials are provided, and biochar ash particles are obtained after pyrolysis; waste incineration bottom ash is provided, and waste incineration bottom ash particles are obtained after natural weathering and air drying; mixing the charcoal ash particles, the waste incineration bottom ash particles, cement and a mineral admixture according to a mass ratio of (0.1-0.5): 7: 1: (1.5-1.9) to obtain a mixture; and carrying out cold bonding granulation on the mixture, and curing to obtain the carbon capture aggregate. The charcoal is added into the aggregate, so that emission of carbon dioxide in the hydration process can be reduced, and the carbon sequestration capacity of the aggregate is enhanced; the biochar can promote cement hydration and formation of hydration products through an internal curing effect, and an internal and external synergistic effect is generated through external carbonization curing, so that the carbonization degree is enhanced, and the mechanical property and the mechanical strength of the aggregate are enhanced. SHENZHEN UNIVERSITY (CN114716200)|SHENZHEN UNIVERSITY ([CN])|(CN114716200)|SHENZHEN UNIVERSITY ([CN]) LIU JUN|LIU GUANG|XING FENG|LI ZHENLIN (CN114716200)|LIU JUN|LIU GUANG|XING FENG|LI ZHENLIN|(CN114716200)|LIU JUN|LIU GUANG|XING FENG|LI ZHENLIN (CN114716200)|ZHU YANGBO;JOHNSON IP|Reg. Nb: 44268 (CN114716200)|The aggregate prepared by the preparation method completely meets various performance requirements of the high-strength light coarse aggregate, can replace natural light aggregate (pumice, shale and the like) and sintered light aggregate (steel slag powder sintered aggregate, ceramsite and the like) to be used as a raw material of light aggregate concrete, reduces the exploitation of the natural light aggregate on one hand, and can effectively save resources; on the other hand, compared with the energy consumed by sintering the ceramsite at thousands of ℃ in the prior art, the aggregate is prepared by a cold bonding method, so that the method is extremely low in energy consumption and pollution, and has great advantages in the aspects of energy conservation, environmental protection and the like.|Therefore, it is necessary to provide a carbon dioxide capture and sequestration technology to reduce the concentration of carbon dioxide in the atmosphere, and to find a reasonable waste incineration bottom ash disposal method to reduce the environmental problems such as land pollution and global warming, and to make the waste resources available for reuse.|Therefore, it is of great importance to find artificial aggregates that can replace natural sands.|At present, the main treatment mode of the waste incineration bottom ash is landfill, but the landfill needs to occupy a large amount of land resources; and because the composition of the incineration waste is complex, the bottom ash may contain various heavy metals and inorganic salt substances, and in the landfill or utilization process of the waste incineration bottom ash, harmful components may be leached out under the action of factors such as acid rain and the like, so that the land environment is polluted.|The existing aggregate is generally natural aggregate, such as pebbles, broken stones, river sand and the like, but with the over-mining of mines, rivers and the like, the natural resource of the aggregate is increasingly deficient, so that the use cost of the natural aggregate is increased.|The waste incineration bottom ash is complex in raw material source and may contain a plurality of heavy metal elements, so that the metal in the bottom ash can be recycled through magnetic separation, and the next step of crushing is facilitated.| (CN114716200)|1. A method for preparing carbon capture aggregate by taking biochar and bottom ash as raw materials is characterized by comprising the following steps:providing a waste biomass raw material, and pyrolyzing the waste biomass raw material to obtain charcoal ash particles;providing waste incineration bottom ash, and naturally weathering and air-drying the waste incineration bottom ash to obtain waste incineration bottom ash particles;mixing the biochar ash particles, the waste incineration bottom ash particles, cement and a mineral admixture according to the mass ratio of (0.1-0.5) to (7) to (1.5-1.9) to obtain a mixture;carrying out cold bonding granulation and maintenance on the mixture to obtain the carbon capture aggregate;the waste biomass raw material comprises at least one of waste wood chips, crop residues and biological excrement;the steps of providing the waste biomass raw material and obtaining the biochar ash particles after pyrolysis specifically comprise:providing a waste biomass raw material, grinding and screening the waste biomass raw material to ensure that the particle size of the waste biomass raw material is 0.063-2 mm, and pyrolyzing the waste biomass raw material to obtain biochar ash particles;the particle size of the biochar ash particles is smaller than 2.36mm, and the particle size of the waste incineration bottom ash particles is smaller than 2.36mm;the step of obtaining the carbon capture aggregate after cold bonding granulation and maintenance of the mixture specifically comprises:putting the mixture into a disc granulator for cold bonding granulation to obtain a coarse aggregate blank body, wherein the particle size range of the coarse aggregate blank body is 4.75-16 mm;and curing the coarse aggregate blank at the temperature of 20 +/-2 ℃ and the relative humidity of more than 95% for at least 28 days to obtain the carbon capture aggregate.| (CN114716200)|In view of the defects of the prior art, the invention aims to provide a carbon capturing aggregate using biochar and bottom ash as raw materials and a preparation method thereof, and aims to replace natural aggregate with high-strength light coarse carbon capturing aggregate prepared from biochar and waste incineration bottom ash as raw materials for preparing concrete, and simultaneously realize the improvement of the mechanical property of the aggregate, the capture and the sealing of carbon dioxide and the effective treatment of the waste incineration bottom ash, protect the environment and save resources.|The invention discloses a carbon capture aggregate using biochar and bottom ash as raw materials and a preparation method thereof, wherein the preparation method comprises the following steps: providing a waste biomass raw material, and pyrolyzing the waste biomass raw material to obtain charcoal ash particles; providing waste incineration bottom ash, and naturally weathering and air-drying the waste incineration bottom ash to obtain waste incineration bottom ash particles; mixing biochar ash particles, garbage incineration bottom ash particles, cement and a mineral admixture according to the mass ratio of (0.1-0.5) to (7) to (1.5-1.9) to obtain a mixture; and carrying out cold bonding granulation and maintenance on the mixture to obtain the carbon capture aggregate.|The invention relates to the technical field of concrete, in particular to carbon capture aggregate taking biochar and bottom ash as raw materials and a preparation method thereof.| (CN114716200)|BOTTOM ASH(100,85)|BIOCHAR(100,36)|BIOCHAR ASH PARTICLE(100,30)|RAW MATERIAL(100,25)|CARBON CAPTURE AGGREGATE(100,18)|COLD BONDING GRANULATION(74,12)|CARBON CAPTURE(64,20)|WASTE INCINERATION(62,67)|CHARCOAL ASH PARTICLE(56,11)|NATURAL AGGREGATE(50,4)|COARSE CARBON CAPTURING AGGREGATE(49,1)|INCINERATION WASTE(42,1)|MINERAL ADMIXTURE(41,15)|WASTE BIOMASS RAW MATERIAL(40,24)|ARTIFICIAL AGGREGATE(40,1)|COARSE AGGREGATE BLANK(38,13)|WASTE INCINERATION BOTTOM ASH(37,44)|DISC GRANULATOR(37,10)|WASTE RESOURCE(36,1)|RIVER SAND(35,1)|EXCREMENT(34,1)|LANDFILL(33,4)|EARTH RESOURCE(33,2)|INORGANIC SALT SUBSTANCE(32,1)|AGGREGATE NATURAL RESOURCE(31,1)|SINTERED AGGREGATE(30,3)|SEQUESTRATION(29,1)|SOIL ENVIRONMENT(29,1)|AGGREGATE(27,25)|SAVE RESOURCE(26,3)|BROKEN ROCK(26,1)|NATURAL SAND(26,1)|BOTTOM ASH PARTICLE(25,22)|GARBAGE INCINERATION(25,2)|CERAMSITE(24,5)|CEMENT(21,14)|COARSE AGGREGATE(21,8)|SINTERED LIGHT AGGREGATE(21,3)|HARMFUL COMPONENT(21,1)|WASTE WOOD CHIP(20,7)|NATURAL LIGHT AGGREGATE EXPLOITATION(20,2)|AGGREGATE CARBON FIXING CAPACITY(20,1)|CARBON DIOXIDE CAPTURE(20,1)|DISC GRANULATOR INCLINATION ANGLE(19,2)|GARBAGE INCINERATION BOTTOM ASH(19,2)|PEBBLE(19,1)|CRUSHING(18,4)|STEEL SLAG(18,4)|LAND POLLUTION(18,1)|CONCRETE(17,6)|PERFORMANCE REQUIREMENT(17,3)|BOTTOM ASH DISPOSAL(17,1)|MINE(17,1)|RIVER(17,1)|TREATMENT MODE(17,1)|NATURAL LIGHT AGGREGATE(16,5)|PYROLYSIS(16,5)|AGGREGATE MECHANICAL PROPERTY(15,3)|TETRACALCIUM ALUMINO FERRITE(15,2)|GRINDING(14,3)|LIGHT AGGREGATE CONCRETE(14,3)|MINERAL ADMIXTURE VOLCANIC ASH(14,3)|GLOBAL WARMING(14,2)|HYDRATION PRODUCT(13,7)|CONTAMINATION(13,4)|INTERNAL CURING(13,4)|CROP RESIDUE(13,3)|CARBON DIOXIDE(12,19)|PORTLAND CEMENT(12,11)|CARBON DIOXIDE EMISSION(12,7)|CARBON DIOXIDE SEALING(12,3)|CARBONIZATION DEGREE ENHANCEMENT(12,3)|PUMICE(12,3)|NATURAL WEATHERING(11,6)|SHALE(11,3)|ENERGY CONSERVATION(11,2)|NATURAL RESOURCE(11,2)|WASTE BIOMASS FEEDSTOCK(11,2)|PARTICLE SIZE(10,18)|ENVIRONMENTAL PROTECTION(10,5)|PYROLYSIS TEMPERATURE(10,5)|INORGANIC POLLUTANT(10,4)|MORAL NATURAL MONTH(10,3)|BIOCHAR ADSORPTION CAPACITY(10,2)|RESIDUAL ASH SLAG(10,2)|ACID RAIN(10,1)|BIOCHAR ASH PARTICLE PRODUCTIVITY(10,1)|AGGREGATE MECHANICAL STRENGTH(9,5)|DICALCIUM SILICATE(9,3)|MAGNET SEPARATOR(9,3)|BIOCHAR ASH PARTICLE PORE(9,1)|MASS RATIO(8,8)|MECHANICAL PROPERTY(8,7)|HEAVY METAL(8,6)|PREPARING AGGREGATE(8,6)|EDGE HEIGHT(8,2)|SINTERED CERAMSITE(8,2)|TRICALCIUM SILICATE(8,2)|MINERAL ADMIXTURE HYDRATION(8,1)|MAGNETIC SEPARATION(7,12)|GRANULATION(7,7)|ECONOMIC BENEFIT(7,3)|LIGHTWEIGHT AGGREGATE(7,2)|FINE BIOMASS FEEDSTOCK(7,1)|ENVIRONMENTAL POLLUTION(6,5)|ENERGY CONSUMPTION(6,4)|EXPERIMENTAL ENVIRONMENT(6,3)|GRANULATED LIGHT COARSE AGGREGATE(6,3)|INORGANIC POWDER(6,3)|INORGANIC SALT(6,3)|LIGHT COARSE AGGREGATE BLANK(6,3)|MOIST COOLING TREATMENT(6,3)|MSW INCINERATION POWER PLANT(6,3)|STANDARD SIEVE(6,3)|AGGREGATE CAPABILITY(6,2)|INCINERATION ELECTRICITY GENERATION(6,2)|BIOCHAR ASH PARTICLE CONTENT(6,1)|URBAN GARBAGE(6,1)|RELATIVE HUMIDITY(5,6)|CARBON DIOXIDE ADSORPTION PERFORMANCE(5,4)|MUFFLE FURNACE(5,4)|AGGREGATE CARBON FIXING CAPABILITY(5,2)|LIGHTER MASS(5,2)|MANURE(5,2)|AGGREGATE ADMIXTURE(5,1)|AGGREGATE INTERNAL HYDRATION(5,1)|AGGREGATE MOLDING(5,1)|BIOMASS WASTE(5,1)|DISC PELLETIZER(5,1)|EMISSION POLLUTION(5,1)|FINAL AGGREGATE PRODUCTIVITY(5,1)|PREPARED CHARCOAL ASH PARTICLE(5,1)|AIR DRYING(4,5)|ENVIRONMENTAL PROTECTION BENEFIT(4,3)|ETTRINGITE(4,3)|BATCH CHARGING(4,1)|BIOCHAR TREATMENT(4,1)|CEMENT HYDRATION SPEED(4,1)|GLACIER MELTING(4,1)|INORGANIC FINE(4,1)|MAGNETIC SEPARATOR CONVEYER BELT(4,1)|OUTDOOR ENVIRONMENT(4,1)|PARTICLE UNIFORMITY(4,1)|RAW MATERIAL SOURCE(4,1)|STEEL SLAG POWDER(4,1)|WASTE UTILIZATION(4,1)|WATERPROOF ENVIRONMENT(4,1)|CARBON DIOXIDE ADSORPTION CAPACITY(3,2)|INSIDE PORE(3,2)|LIGHT BIOLOGICAL CARBON(3,2)|LIGHTER WEIGHT(3,2)|REFUSE INCINERATION BOTTOM ASH(3,2)|SOLIDIFICATION(3,2)|TRICALCIUM ALUMINATE(3,2)||(CN114716200)|BOTTOM ASH(100,81)|BIOCHAR(100,39)|BIOCHAR ASH PARTICLE(100,29)|RAW MATERIAL(100,25)|CARBON CAPTURE AGGREGATE(100,22)|CARBON CAPTURE(78,17)|WASTE INCINERATION(74,67)|COLD BONDING GRANULATION(66,10)|CHARCOAL ASH PARTICLE(65,13)|NATURAL AGGREGATE(59,4)|COARSE CARBON CAPTURING AGGREGATE(58,1)|INCINERATION WASTE(49,1)|MINERAL ADMIXTURE(48,15)|ARTIFICIAL AGGREGATE(47,1)|HARMFUL INGREDIENT(44,1)|WASTE INCINERATION BOTTOM ASH(43,43)|WASTE RESOURCE(43,1)|RIVER SAND(41,1)|LANDFILL(39,4)|EARTH RESOURCE(39,2)|INORGANIC SALT SUBSTANCE(38,1)|AGGREGATE NATURAL RESOURCE(37,1)|DISC GRANULATOR(36,11)|SINTERED AGGREGATE(35,3)|SEQUESTRATION(35,1)|SOIL ENVIRONMENT(35,1)|WASTE BIOMASS RAW MATERIAL(33,23)|AGGREGATE(32,25)|BOTTOM ASH PARTICLE(31,24)|SAVE RESOURCE(31,3)|BROKEN ROCK(31,1)|NATURAL SAND(30,1)|CERAMSITE(28,5)|CEMENT(26,14)|SINTERED LIGHT AGGREGATE(25,3)|NATURAL LIGHT AGGREGATE EXPLOITATION(24,2)|AGGREGATE CARBON FIXING CAPACITY(24,1)|CARBON DIOXIDE CAPTURE(24,1)|PEBBLE(23,1)|NATURAL WEATHERING(22,7)|CRUSHING(22,4)|LAND POLLUTION(22,1)|STEEL SLAG(21,4)|BOTTOM ASH DISPOSAL(21,1)|RIVER(21,1)|TREATMENT MODE(21,1)|COARSE AGGREGATE(20,9)|PERFORMANCE REQUIREMENT(20,3)|MINE(20,1)|NATURAL LIGHT AGGREGATE(19,5)|AGGREGATE MECHANICAL PROPERTY(18,3)|TETRACALCIUM ALUMINO FERRITE(18,2)|WASTE WOOD CHIP(17,7)|LIGHT AGGREGATE CONCRETE(17,3)|MANURE(17,3)|GLOBAL WARMING(17,2)|HYDRATION PRODUCT(16,7)|INTERNAL CURING(16,4)|MINERAL ADMIXTURE VOLCANIC ASH(16,3)|CONTAMINATION(15,4)|CARBON DIOXIDE SEALING(15,3)|CARBONIZATION DEGREE ENHANCEMENT(15,3)|CARBON DIOXIDE(14,19)|PORTLAND CEMENT(14,10)|CARBON DIOXIDE EMISSION(14,7)|CONCRETE(14,4)|WASTE BIOMASS MATERIAL(14,4)|PUMICE(14,3)|SHALE(14,3)|ENERGY CONSERVATION(13,2)|NATURAL RESOURCE(13,2)|WASTE BIOMASS FEEDSTOCK(13,2)|PYROLYSIS TEMPERATURE(12,5)|INORGANIC POLLUTANT(12,4)|MORAL NATURAL MONTH(12,3)|BIOCHAR ADSORPTION CAPACITY(12,2)|RESIDUAL ASH SLAG(12,2)|ACID RAIN(12,1)|BIOCHAR ASH PARTICLE PRODUCTIVITY(12,1)|AGGREGATE MECHANICAL STRENGTH(11,5)|ENVIRONMENTAL PROTECTION(11,5)|DICALCIUM SILICATE(11,3)|GRINDING(11,3)|MAGNET SEPARATOR(11,3)|CONCRETE RAW MATERIAL(11,1)|MASS RATIO(10,8)|MECHANICAL PROPERTY(10,7)|HEAVY METAL(10,6)|PREPARING AGGREGATE(10,6)|MUNICIPAL WASTE INCINERATION(10,2)|ROTATING SPEED(10,2)|SINTERED CERAMSITE(10,2)|TRICALCIUM SILICATE(10,2)|MAGNETIC SEPARATION(9,12)|AIR DRYING(9,6)|CROP RESIDUE(9,3)|EDGE HEIGHT(9,3)|LIGHTWEIGHT AGGREGATE(9,2)|MINERAL ADMIXTURE HYDRATION(9,1)|PARTICLE SIZE(8,18)|ECONOMIC BENEFIT(8,3)|FINE BIOMASS FEEDSTOCK(8,1)|ENVIRONMENTAL POLLUTION(7,5)|ENERGY CONSUMPTION(7,4)|EXPERIMENTAL ENVIRONMENT(7,3)|GRANULATED LIGHT COARSE AGGREGATE(7,3)|INORGANIC POWDER(7,3)|INORGANIC SALT(7,3)|LIGHT COARSE AGGREGATE BLANK(7,3)|MOIST COOLING TREATMENT(7,3)|MSW INCINERATION POWER PLANT(7,3)|AGGREGATE CAPABILITY(7,2)|BIOCHAR ASH PARTICLE CONTENT(7,1)|URBAN GARBAGE(7,1)|CARBON DIOXIDE ADSORPTION PERFORMANCE(6,4)|MUFFLE FURNACE(6,4)|STANDARD SIEVE(6,3)|AGGREGATE CARBON FIXING CAPABILITY(6,2)|AGGREGATE ADMIXTURE(6,1)|AGGREGATE INTERNAL HYDRATION(6,1)|AGGREGATE MOLDING(6,1)|BIOMASS WASTE(6,1)|EMISSION POLLUTION(6,1)|FINAL AGGREGATE PRODUCTIVITY(6,1)|PREPARED CHARCOAL ASH PARTICLE(6,1)|ENVIRONMENTAL PROTECTION BENEFIT(5,3)|ETTRINGITE(5,3)|LIGHTER WEIGHT(5,3)|BATCH CHARGING(5,1)|BIOCHAR TREATMENT(5,1)|CEMENT HYDRATION SPEED(5,1)|DISC GRANULATOR INCLINATION ANGLE(5,1)|GLACIER MELTING(5,1)|INORGANIC FINE(5,1)|MAGNETIC SEPARATOR CONVEYER BELT(5,1)|OUTDOOR ENVIRONMENT(5,1)|PARTICLE UNIFORMITY(5,1)|RAW MATERIAL SOURCE(5,1)|STEEL SLAG POWDER(5,1)|WASTE UTILIZATION(5,1)|WATERPROOF ENVIRONMENT(5,1)|COMPRESSIVE STRENGTH(4,4)|CARBON DIOXIDE ADSORPTION CAPACITY(4,2)|CONTENT ACCOUNT(4,2)|INSIDE PORE(4,2)|SOLIDIFICATION(4,2)|TRICALCIUM ALUMINATE(4,2)|AGGREGATE CARBON CAPTURE CAPACITY(4,1)| (CN114716200)|1. A method for preparing carbon capture aggregate by taking biochar and bottom ash as raw materials is characterized by comprising the following steps:|providing a waste biomass raw material, and pyrolyzing the waste biomass raw material to obtain charcoal ash particles;|providing waste incineration bottom ash, and naturally weathering and air-drying the waste incineration bottom ash to obtain waste incineration bottom ash particles;|mixing the biochar ash particles, the waste incineration bottom ash particles, cement and a mineral admixture according to the mass ratio of (0.1-0.5) to (7) to (1.5-1.9) to obtain a mixture;|carrying out cold bonding granulation and maintenance on the mixture to obtain the carbon capture aggregate;|the waste biomass raw material comprises at least one of waste wood chips, crop residues and biological excrement;|the steps of providing the waste biomass raw material and obtaining the biochar ash particles after pyrolysis specifically comprise:|providing a waste biomass raw material, grinding and screening the waste biomass raw material to ensure that the particle size of the waste biomass raw material is 0.063-2 mm, and pyrolyzing the waste biomass raw material to obtain biochar ash particles;|the particle size of the biochar ash particles is smaller than 2.36mm, and the particle size of the waste incineration bottom ash particles is smaller than 2.36mm;|the step of obtaining the carbon capture aggregate after cold bonding granulation and maintenance of the mixture specifically comprises:|putting the mixture into a disc granulator for cold bonding granulation to obtain a coarse aggregate blank body, wherein the particle size range of the coarse aggregate blank body is 4.75-16 mm;|and curing the coarse aggregate blank at the temperature of 20 +/-2 ℃ and the relative humidity of more than 95% for at least 28 days to obtain the carbon capture aggregate.|2. The method for preparing carbon capturing aggregate using bio-char and bottom ash as raw materials according to claim 1, wherein the pyrolysis temperature is 500-700 ℃ and the time is 2 hours.|3. The method for preparing the carbon capturing aggregate from the biochar and the bottom ash as the raw materials according to claim 1, wherein the specific steps of providing the waste incineration bottom ash, and naturally weathering and air drying the waste incineration bottom ash to obtain the waste incineration bottom ash particles comprise:|providing waste incineration bottom ash, carrying out magnetic separation, naturally weathering and air drying for 28-35 days, crushing, and screening to obtain waste incineration bottom ash particles.|4. The method for producing a carbon-capturing aggregate from biochar and bottom ash as raw materials according to claim 1, wherein the cement is portland cement.|5. The method for preparing carbon capturing aggregate using biochar and bottom ash as raw materials according to claim 1, wherein the inclination angle of the disc granulator is 45-60 °, the diameter of the disc is 1m, the edge height is 1.5cm, and the rotation speed is 35-55 rpm.|6. A carbon capturing aggregate using biochar and bottom ash as raw materials, characterized in that the carbon capturing aggregate is prepared by the preparation method according to any one of claims 1 to 5. (CN114716200)|TECHNICAL FIELD|[0001] The invention relates to the technical field of concrete, in particular to carbon capture aggregate taking biochar and bottom ash as raw materials and a preparation method thereof.|BACKGROUND ART|[0002] The aggregate is a basic raw material for preparing concrete, approximately accounts for two thirds of the total mass of the concrete, and the demand of the aggregate is gradually increased along with the rapid increase of the annual use amount of the concrete. The existing aggregate is generally natural aggregate, such as pebbles, broken stones, river sand and the like, but with the over-mining of mines, rivers and the like, the natural resource of the aggregate is increasingly deficient, so that the use cost of the natural aggregate is increased. Therefore, it is of great importance to find artificial aggregates that can replace natural sands.|[0003] At present, due to the increase of the emission amount of carbon dioxide, global warming is increasingly serious, and the problems of severe drought, rainfall mode change, extreme heat waves, glacier melting, sea level rising and the like occur. The construction industry is one of the industries with serious carbon dioxide emission, and the total emission of the cement industry is estimated to account for nearly 8% of the global carbon dioxide emission.|[0004] The urban garbage is increased along with the continuous promotion of the urbanization process, and about 80 percent of the residual ash slag after the garbage is burnt is bottom ash, and 20 percent of the residual ash slag is fly ash. At present, the main treatment mode of the waste incineration bottom ash is landfill, but the landfill needs to occupy a large amount of land resources; and because the composition of the incineration waste is complex, the bottom ash may contain various heavy metals and inorganic salt substances, and in the landfill or utilization process of the waste incineration bottom ash, harmful components may be leached out under the action of factors such as acid rain and the like, so that the land environment is polluted.|[0005] Therefore, it is necessary to provide a carbon dioxide capture and sequestration technology to reduce the concentration of carbon dioxide in the atmosphere, and to find a reasonable waste incineration bottom ash disposal method to reduce the environmental problems such as land pollution and global warming, and to make the waste resources available for reuse.|DISCLOSURE|Disclosure of Invention|[0006] In view of the defects of the prior art, the invention aims to provide a carbon capturing aggregate using biochar and bottom ash as raw materials and a preparation method thereof, and aims to replace natural aggregate with high-strength light coarse carbon capturing aggregate prepared from biochar and waste incineration bottom ash as raw materials for preparing concrete, and simultaneously realize the improvement of the mechanical property of the aggregate, the capture and the sealing of carbon dioxide and the effective treatment of the waste incineration bottom ash, protect the environment and save resources.|[0007] The technical scheme of the invention is as follows:|[0008] in a first aspect of the present invention, there is provided a method for preparing a carbon-capturing aggregate using biochar and bottom ash as raw materials, comprising the steps of:|[0009] providing a waste biomass raw material, and pyrolyzing the waste biomass raw material to obtain charcoal ash particles;|[0010] providing waste incineration bottom ash, and naturally weathering and air-drying the waste incineration bottom ash to obtain waste incineration bottom ash particles;|[0011] mixing the biochar ash particles, the waste incineration bottom ash particles, cement and a mineral admixture according to the mass ratio of (0.1-0.5) to (7) to (1.5-1.9) to obtain a mixture;|[0012] and carrying out cold bonding granulation and maintenance on the mixture to obtain the carbon capture aggregate.|[0013] Optionally, the waste biomass feedstock comprises at least one of waste wood chips, crop residues, biological manure.|[0014] Optionally, the step of providing the waste biomass raw material and obtaining the biochar ash particles after pyrolysis specifically includes: providing a waste biomass raw material, grinding and screening the waste biomass raw material to ensure that the particle size of the waste biomass raw material is 0.063-2 mm, and obtaining biochar ash particles after pyrolysis.|[0015] Optionally, the pyrolysis temperature is 500-700 ℃ and the time is 2h.|[0016] Optionally, the particle size of the biochar ash particles is less than 2.36mm, and the particle size of the waste incineration bottom ash particles is less than 2.36mm.|[0017] Optionally, the specific steps of providing the waste incineration bottom ash, and obtaining the waste incineration bottom ash particles after natural weathering and air drying include:|[0018] providing waste incineration bottom ash, carrying out magnetic separation, naturally weathering and air drying for 28-35 days, crushing, and screening to obtain waste incineration bottom ash particles.|[0019] Optionally, the cement is portland cement.|[0020] Optionally, the step of obtaining the carbon capturing aggregate after cold bonding, granulation and curing of the mixture specifically includes:|[0021] putting the mixture into a disc granulator for cold bonding granulation to obtain a coarse aggregate blank body, wherein the particle size range of the coarse aggregate blank body is 4.75-16 mm;|[0022] and curing the coarse aggregate blank for at least 28 days under the conditions that the temperature is 20 +/-2 ℃ and the relative humidity is more than 95 percent to obtain the carbon capture aggregate.|[0023] Optionally, the inclination angle of the disc granulator is 45-60 degrees, the diameter of the disc is 1m, the edge height is 1.5cm, and the rotating speed is 35-55 rpm.|[0024] In a second aspect of the present invention, there is provided a carbon capturing aggregate using biochar and bottom ash as raw materials, wherein the carbon capturing aggregate is prepared by the above-described preparation method of the present invention.|[0025] Has the advantages that: the invention provides a preparation method of carbon capturing aggregate by taking biochar and bottom ash as raw materials, wherein biochar is added into the aggregate instead of part of cementing materials, so that the carbon capturing capability of the aggregate can be enhanced, the carbon dioxide emission in the hydration process of the aggregate is reduced, and the carbon fixing capability of the aggregate is enhanced; the high adsorption capacity of the biochar on organic and inorganic pollutants in the waste incineration bottom ash can greatly treat and stabilize the waste incineration bottom ash, and reduce the environmental pollution and the land resource use pressure; meanwhile, the biochar can promote the hydration of cement and the formation of hydration products through the internal curing effect, and generate an internal and external synergistic effect through external carbonization curing to enhance the carbonization degree, so that the mechanical property and the mechanical strength of the aggregate are enhanced. By utilizing the characteristics of porous and light biological carbon and waste incineration bottom ash particles, the prepared aggregate has lighter mass and can be used as light coarse aggregate. The mineral admixture is hydrated with cement to form hydration products such as C-S-H gel, ettringite and the like, so that heavy metals such as Cu, pb, cr and the like in bottom ash and inorganic salts can be well fixed, and the cement bottom ash is green and environment-friendly. The prepared aggregate has high strength and low water absorption rate by utilizing the characteristic of high activity of the volcanic ash of the mineral admixture, combining with the biochar and the waste incineration bottom ash and using cement as a bonding agent. The aggregate prepared by the preparation method completely meets various performance requirements of the high-strength light coarse aggregate, can replace natural light aggregate (pumice, shale and the like) and sintered light aggregate (steel slag powder sintered aggregate, ceramsite and the like) to be used as a raw material of light aggregate concrete, reduces the exploitation of the natural light aggregate on one hand, and can effectively save resources; on the other hand, compared with the energy consumed by sintering the ceramsite at thousands of ℃ in the prior art, the aggregate is prepared by a cold bonding method, so that the method is extremely low in energy consumption and pollution, and has great advantages in the aspects of energy conservation, environmental protection and the like. The invention provides a novel production method of carbon capture aggregate with high economic benefit and environmental protection benefit, which simultaneously realizes the improvement of the mechanical property of the aggregate, the capture and the sealing of carbon dioxide and the effective treatment of waste incineration bottom ash, protects the environment and saves resources.|DRAWINGS DESCRIPTION|[0026] FIG. 1 is a schematic flow chart of a method for preparing carbon-capturing aggregate from biochar and bottom ash according to an embodiment of the present invention.|INVENTION MODE|Detailed Description|[0027] The present invention provides a carbon capturing aggregate using biochar and bottom ash as raw materials and a method for preparing the same, and the present invention is further described in detail below in order to make the objects, technical solutions, and effects of the present invention clearer and clearer. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.|[0028] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.|[0029] The embodiment of the invention provides a preparation method of carbon capture aggregate by taking biochar and bottom ash as raw materials, as shown in figure 1, comprising the following steps:|[0030] s1, providing a waste biomass raw material, and pyrolyzing the waste biomass raw material to obtain charcoal ash particles;|[0031] s2, providing waste incineration bottom ash, and naturally weathering and air-drying the waste incineration bottom ash to obtain waste incineration bottom ash particles;|[0032] s3, mixing the biochar ash particles, the garbage incineration bottom ash particles, cement and mineral admixtures according to the ratio of (0.1-0.5): 7:1: (1.5-1.9) to obtain a mixture;|[0033] and S4, carrying out cold bonding granulation and maintenance on the mixture to obtain the carbon capture aggregate.|[0034] According to the invention, the biochar is added into the aggregate instead of part of cementing materials, so that the carbon capture capacity of the aggregate can be enhanced, the carbon dioxide emission in the aggregate hydration process is reduced, and the carbon fixation capacity of the aggregate is enhanced; the biochar has a mesoporous structure, relatively high surface area and rich functional groups, so that organic and inorganic pollutants in the waste incineration bottom ash can be adsorbed and fixed, and the waste incineration bottom ash can be treated and stabilized in a large amount, so that the aggregate has lighter weight, and the environmental pollution caused by the waste incineration bottom ash and the land resource use pressure caused by landfill of the waste incineration bottom ash are reduced; meanwhile, the biochar can promote the hydration of cement and the formation of hydration products through the internal curing effect (specifically, the porous structure of the biochar can adsorb water inside pores, and then the solidification is promoted and the hydration is improved through releasing water and increasing the internal relative humidity in the curing process, so that the hydration speed of the cement is increased, the hydration degree is improved), and the internal and external synergistic effect is generated through the external carbonization and curing, so that the carbonization degree is enhanced, and the mechanical property and the mechanical strength of the aggregate are enhanced. By utilizing the characteristics of porous and light weight of the biochar and waste incineration bottom ash particles, the prepared aggregate has lighter weight and can be used as light coarse aggregate. Hydration products such as C-S-H gel, ettringite and the like formed by hydration of the mineral admixture and cement can well fix heavy metals such as Cu, pb, cr and the like and inorganic salts in bottom ash, and the cement is green and environment-friendly. The aggregate prepared by utilizing the characteristic of strong activity of the mineral admixture volcanic ash, combining the mineral admixture with biochar and waste incineration bottom ash and adopting the cold bonding granulation technology through taking cement as a bonding agent has higher strength and lower water absorption. The aggregate prepared by the preparation method completely meets various performance requirements of the high-strength light coarse aggregate, and can replace natural light aggregates (pumice, shale and the like) and sintered light aggregates (steel slag powder sintered aggregates, ceramsite and the like) as the raw materials of the light aggregate concrete.|[0035] In step S1, in one embodiment, the waste biomass material includes at least one of waste wood chips, crop residues, and biological manure, but is not limited thereto. The biochar prepared from the waste biomass raw materials has a mesoporous structure, a relatively large surface area and rich functional groups, can adsorb and fix organic and inorganic pollutants in waste incineration bottom ash, can treat and stabilize the waste incineration bottom ash in a large amount, enables the aggregate to be lighter in weight, can adsorb water inside pores, and promotes solidification and improves hydration by releasing water and increasing internal relative humidity in a curing process, so that the cement hydration speed is increased, and the hydration degree is improved.|[0036] In one embodiment, the step of providing the waste biomass feedstock and obtaining the biochar ash particles after pyrolysis specifically comprises: providing a waste biomass raw material, grinding and screening the waste biomass raw material to ensure that the particle size of the waste biomass raw material is 0.063-2 mm, and pyrolyzing the waste biomass raw material to obtain the biochar ash particles. The use of finer biomass feedstock can increase the productivity of the biochar ash particles.|[0037] In one embodiment, the pyrolysis temperature is 500 to 700 ℃ and the time is 2 hours. The pyrolysis temperature is not too high or too low, and the pores of the biochar ash particles are too large due to too high temperature, so that the strength of the aggregate is influenced; too low a temperature results in a reduction in the carbon dioxide adsorption capacity of the biochar ash particles. Pyrolysis at a temperature in the range of 500 ℃ to 700 ℃ is the most suitable temperature for the biochar ash particles as an aggregate admixture. Specifically, the waste biomass raw material is placed in a muffle furnace, and the temperature is raised to 500-700 ℃ at a heating rate of 10 ℃/min and is kept for 2h. Preferably, the temperature of the pyrolysis is 600 ℃.|[0038] In specific implementation, the prepared charcoal ash particles are soaked in water at 100 ℃ for 0.5 hour until the charcoal ash particles are completely saturated, then vacuum drying and filtering are carried out to obtain saturated surface drying conditions, and then the charcoal ash particles are put into a transparent plastic bag to be sealed and stored for later use.|[0039] In one embodiment, the biochar ash particles have a particle size of less than 2.36mm to make them suitable for cold-bond pelletizing.|[0040] In step S2, in an embodiment, the specific steps of providing the waste incineration bottom ash, and obtaining the waste incineration bottom ash particles through natural weathering and air drying include:|[0041] providing waste incineration bottom ash, carrying out magnetic separation, naturally weathering and air drying for 28-35 days, crushing and screening to obtain waste incineration bottom ash particles. The waste incineration bottom ash is complex in raw material source and may contain a plurality of heavy metal elements, so that the metal in the bottom ash can be recycled through magnetic separation, and the next step of crushing is facilitated. The process can be used for specifically placing the waste incineration bottom ash on a conveyor belt of a magnetic separator, and then starting the magnetic separator for automatic magnetic separation. The natural weathering and the air drying are carried out simultaneously, the aim is to reduce the heavy metal in the bottom ash of the waste incineration, and the natural weathering and the air drying can be carried out in an outdoor and rainproof environment. Preferably, the natural weathering and air drying time is 30 days.|[0042] In one embodiment, the particle size of the waste incineration bottom ash particles is less than 2.36mm. The bottom ash with larger particle size can be directly used as a coarse aggregate to be applied to engineering, while the particles smaller than 2.36mm are difficult to treat, and the part accounts for more than 50 percent of the total amount of the bottom ash. In addition, the cold bonding technique is only suitable for the treatment of fine particulate matter, so bottom ash particles with a particle size of less than 2.36mm are selected.|[0043] In the step S3, the biochar ash particles, the waste incineration bottom ash particles, the cement and the mineral admixture are mixed according to the proportion of (0.1-0.5): 7:1: (1.5-1.9) to obtain a mixture. Too high a content of biochar ash particles leads to too high a porosity and a reduction in the mechanical strength of the aggregate. Under the proportion, the prepared aggregate has high production efficiency, uniform particle size distribution and high strength; moreover, the carbon dioxide adsorption capacity of the biochar can be stably exerted, and simultaneously, a large amount of waste incineration bottom ash can be treated, so that the economic cost is reduced, and the pollution to the environment caused by treating the waste incineration bottom ash is reduced. Preferably, the biochar ash particles, the waste incineration bottom ash particles, the cement and the mineral admixture are mixed according to the mass ratio of 0.3.|[0044] In one embodiment, the mineral admixture is preferably mineral fines. The reason is that the mineral powder has higher activity, and can well enhance the strength of the aggregate and reduce the water absorption of the aggregate.|[0045] In one embodiment, the cement is portland cement, but is not limited thereto. The main mineral compositions of portland cement are: tricalcium silicate, dicalcium silicate, tricalcium aluminate, tetracalcium aluminoferrite. Tricalcium silicate determines the strength of portland cement within four weeks; the strength of the dicalcium silicate is exerted after four weeks, and the strength of the dicalcium silicate reaches four weeks about one year; tricalcium aluminate develops strength faster but has lower strength, and plays a certain role in the strength of portland cement within 1 to 3 days or a little longer time; tetracalcium aluminoferrite also develops strength quickly, but has low strength and contributes little to the strength of portland cement.|[0046] In step S4, granulation is performed by adopting a cold bonding granulation technology. The cold bonding granulation technology has the advantages of low energy consumption and less pollutant emission, and has great advantages compared with sintered ceramsite requiring thousands of degrees centigrade and the like. The cold bonding granulation technology can recycle solid wastes, reduce the carbon dioxide emission in the aggregate preparation process and the environmental burden brought by solid waste landfill, and the product can replace natural aggregates, thereby effectively saving natural resources. Therefore, the cold bonding technology is applied to the treatment of the biochar and the municipal refuse incineration bottom ash, the biochar and the municipal refuse incineration bottom ash can be made into aggregate to be applied to concrete, the waste utilization can be realized, and the environmental pollution and the occupation of land resources are reduced.|[0047] In one embodiment, the step of obtaining the carbon capturing aggregate after cold binding granulation and curing of the mixture specifically comprises:|[0048] s41, putting the mixture into a disc granulator for cold bonding granulation to obtain a coarse aggregate blank body, wherein the particle size range of the coarse aggregate blank body is 4.75-16 mm;|[0049] s42, curing the coarse aggregate blank for at least 28 days at the temperature of 20 +/-2 ℃ and the relative humidity of more than 95% to obtain the carbon capture aggregate.|[0050] In step S41,4.75mm is the defined particle size of the coarse aggregate, and aggregates larger than 4.75mm are generally considered to be coarse aggregates. Further, since the aggregate is artificial, the strength of the aggregate tends to be rather lowered as the particle diameter is larger, and the strength of the aggregate having a particle diameter of more than 16mm is remarkably lowered. Therefore, the particle size range of the coarse aggregate blank is selected to be 4.75-16mm.|[0051] In specific implementation, the mixture is put into a disc granulator for stirring, water is uniformly sprayed on the mixture in the stirring process, the mass ratio of the total water consumption to the mixture is 20% -22% (when the ratio of the water to the mixture is too high or too low, the molding of the aggregate is greatly influenced, so that a proper aggregate cannot be produced or the granulation efficiency is low), and the proper rotation speed is kept, so that the mixture is fully polymerized under the action of moisture and centrifugation, and finally a coarse aggregate blank is obtained. In order to fully mix the raw materials, powdery materials such as biochar, waste incineration bottom ash and the like are put on a disc and stirred for about 5-10 minutes until the color is uniform and no obvious particles exist. In specific implementation, a part of the mixture is required to be reserved before the mixture is put into the disc granulator, and the mixture is added according to the proportion of the dry and wet conditions of the mixture in the subsequent water adding and mixing process. The final aggregate productivity and particle uniformity can be effectively improved by batch charging.|[0052] In one embodiment, the disk pelletizer has a disk inclination of 45 to 60 °, a disk diameter of 1m, a rim height of 1.5cm, and a rotational speed of 35 to 55rpm.|[0053] In step S42, the concrete can be maintained in water bath at different temperatures (20-80 ℃). The water bath maintenance can provide sufficient water, so that the internal hydration of the aggregate is sufficient, and the performance of the aggregate can be obviously enhanced. Wherein, the temperature is not suitable to be too high or too low; high temperature can cause the moisture of the aggregate to evaporate, and the performance of the aggregate is reduced; low temperatures can inhibit hydration, which in turn affects aggregate performance.|[0054] The embodiment of the invention also provides a carbon capturing aggregate which takes the biochar and the bottom ash as raw materials, wherein the carbon capturing aggregate is prepared by the preparation method disclosed by the embodiment of the invention. The single-particle compressive strength of the carbon capturing aggregate is 2.44-2.70 MPa, the carbon dioxide adsorption performance is 6.4-7.6 mmol/g, and the water absorption rate is 14.25-16.32%. According to the specification of GB T17431.1-lightweight aggregate and test method part 1 thereof, the carbon-capturing aggregate can be considered as lightweight aggregate, and according to the specification, the cylinder pressure strength of the aggregate meets the requirements of high-strength lightweight coarse aggregate. Compared with most commercial light coarse aggregates on the market, the aggregate prepared by the invention has higher strength and better performance; the water absorption rate is low, and the requirements of subsequent products can be met; the method has extremely high economic benefit and environmental protection benefit, and the biomass waste and the waste incineration bottom ash are recycled, so that the material cost is reduced and the environmental pollution is reduced; meanwhile, the aggregate is prepared by a cold bonding method, so that the energy consumption is extremely low, the pollution is less, and the method has great advantages compared with sintered ceramsite requiring thousands of degrees centigrade and the like.|[0055] The invention is further illustrated by the following specific examples.|[0056] In the following examples, the biochar ash particles used in the raw material were prepared by high temperature pyrolysis using waste wood chips with a particle size ranging from 0.063mm to 2mm as the raw material; the waste incineration bottom ash is the bottom ash produced by a waste incineration power plant, and bottom ash particles with the size smaller than 2.36mm are selected after magnetic separation, natural weathering and air drying; other raw materials, such as mineral admixture (selected from mineral powder or steel slag powder) and portland cement, are commercially available. The starting material compound composition is shown in table 1:|[0057] table 1: composition of raw Material Compounds|[0058] |[0059] Example 1:|[0060] sieving the waste wood chips to obtain the waste wood chips with the particle size of 0.063 mm-2 mm, then putting the waste wood chips into a muffle furnace for high-temperature pyrolysis at the heating rate of 10 ℃/min, keeping the temperature for two hours after the temperature is raised to 600 ℃ to obtain charcoal ash particles, soaking the charcoal ash particles in water with the temperature of 100 ℃ after cooling for 0.5 hour, then completely saturating the charcoal ash particles, and then drying the charcoal ash particles through vacuum filtration to obtain saturated surface drying conditions;|[0061] carry out moist cooling treatment after carrying out the magnetic separation from the remaining end ash after the incineration electricity generation that the msw incineration power plant was collected through the magnet separator, put it 1 natural month of morals and air-dry under natural condition again, then carry out screening: under the condition of 20 +/-2 ℃ of experimental environment, bottom ash passes through standard sieves of 37.5mm, 31.5mm, 26.5mm, 19mm, 16mm, 9.5mm, 4.75mm and 2.36mm, bottom ash (the content of the bottom ash accounts for more than 50 percent of the total volume) below 2.36mm is selected, and the rest of the bottom ash is crushed to 2.36mm after magnetic separation. Mixing biochar ash particles, mineral powder, portland cement and waste incineration bottom ash in a proportion of 0.1:1.9:1:7, fully mixing in a mass ratio;|[0062] the mixed raw materials are put into a disc granulator for granulation to obtain a light coarse aggregate blank body with the thickness of 4.75-16 mm;|[0063] and placing the granulated light coarse aggregate blank in an environment with the temperature of 20 +/-2 ℃ and the relative humidity of 95% for curing for 28 days to obtain the high-strength carbon capture aggregate.|[0064] Through tests, the single-particle compressive strength of the obtained carbon capture aggregate is 2.47MPa, the water absorption is 15.43%, and the carbon dioxide adsorption performance is 6.4mmol/g.|[0065] Example 2:|[0066] sieving the waste wood scraps to obtain the waste wood scraps with the grain size of 0.063 mm-2 mm, then putting the waste wood scraps into a muffle furnace for high-temperature pyrolysis at the heating rate of 10 ℃/min, keeping the temperature for two hours after the temperature is raised to 600 ℃ to obtain biochar ash particles, soaking the biochar ash particles in 100 ℃ water for 0.5 hour after cooling, fully saturating the biochar ash particles, and then drying the biochar ash particles through vacuum filtration to obtain saturated surface drying conditions.|[0067] Carry out moist cooling treatment after carrying out the magnetic separation from the remaining end ash after the incineration power generation that the msw incineration power plant was collected through the magnet separator, put it 1 natural month of morals and air-dry under natural condition again, then sieve and handle: under the condition of 20 +/-2 ℃ of experimental environment, bottom ash passes through standard sieves of 37.5mm, 31.5mm, 26.5mm, 19mm, 16mm, 9.5mm, 4.75mm and 2.36mm, bottom ash (the content of the bottom ash accounts for more than 50 percent of the total volume) below 2.36mm is selected, and the rest of the bottom ash is crushed to 2.36mm after magnetic separation. Mixing biochar ash particles, steel slag powder, portland cement and waste incineration bottom ash in a proportion of 0.3:1.7:1:7, fully mixing in a mass ratio;|[0068] the mixed raw materials are put into a disc granulator for granulation to obtain a light coarse aggregate blank body with the thickness of 4.75-16 mm;|[0069] and placing the granulated light coarse aggregate blank in an environment with the temperature of 20 +/-2 ℃ and the relative humidity of 95% for curing for 28 days to obtain the high-strength carbon capture aggregate.|[0070] Tests show that the compressive strength of the single particle of the obtained carbon capture aggregate is 2.70MPa, the water absorption rate is 16.32 percent, and the carbon dioxide adsorption performance is 7.3mmol/g.|[0071] Example 3:|[0072] sieving the waste wood scraps to obtain waste wood scraps with the particle size of 0.063 mm-2 mm, putting the waste wood scraps into a muffle furnace for high-temperature pyrolysis at the heating rate of 10 ℃/min, keeping the temperature for two hours after the temperature is raised to 600 ℃ to obtain biochar ash particles, cooling, soaking the biochar ash particles in 100 ℃ water for 0.5 hour, fully saturating, and then filtering and drying in vacuum to obtain saturated surface drying conditions;|[0073] carry out moist cooling treatment after carrying out the magnetic separation from the remaining end ash after the incineration electricity generation that the msw incineration power plant was collected through the magnet separator, put it 1 natural month of morals and air-dry under natural condition again, then carry out screening: under the condition of 20 +/-2 ℃ of experimental environment, bottom ash passes through standard sieves of 37.5mm, 31.5mm, 26.5mm, 19mm, 16mm, 9.5mm, 4.75mm and 2.36mm, bottom ash (the content of the bottom ash accounts for more than 50 percent of the total volume) below 2.36mm is selected, and the rest of the bottom ash is crushed to 2.36mm after magnetic separation. Mixing biochar ash particles, mineral powder, portland cement and waste incineration bottom ash in a proportion of 0.5:1.5:1:7, fully mixing in a mass ratio;|[0074] putting the mixed raw materials into a disc granulator for granulation to obtain a light coarse aggregate blank body with the thickness of 4.75-16 mm;|[0075] and placing the granulated light coarse aggregate blank in an environment with the temperature of 20 +/-2 ℃ and the relative humidity of 95% for curing for 28 days to obtain the high-strength carbon capture aggregate.|[0076] Tests show that the compressive strength of the single particle of the obtained carbon capture aggregate is 2.44MPa, the water absorption is 14.25 percent, and the carbon dioxide adsorption performance is 7.6mmol/g.|[0077] In conclusion, the invention provides a preparation method of carbon capturing aggregate by taking biochar and bottom ash as raw materials, and the biochar is added into the aggregate instead of part of cementing materials, so that the carbon capturing capability of the aggregate can be enhanced, the carbon dioxide emission in the hydration process of the aggregate is reduced, and the carbon fixing capability of the aggregate is enhanced; the high adsorption capacity of the biochar on organic and inorganic pollutants in the waste incineration bottom ash can greatly treat and stabilize the waste incineration bottom ash, and reduce the environmental pollution and the land resource use pressure; meanwhile, the biochar can promote cement hydration and improve the formation of hydration products through the internal curing effect, and the internal and external synergistic effect is generated through external carbonization curing to enhance the carbonization degree, so that the mechanical property and the mechanical strength of the aggregate are enhanced. By utilizing the characteristics of porous and light biological carbon and waste incineration bottom ash particles, the prepared aggregate has lighter mass and can be used as light coarse aggregate. The mineral admixture is hydrated with cement to form hydration products such as C-S-H gel, ettringite and the like, so that heavy metals such as Cu, pb, cr and the like in bottom ash and inorganic salts can be well fixed, and the cement bottom ash is green and environment-friendly. The prepared aggregate has high strength and low water absorption rate by utilizing the characteristic of high activity of the volcanic ash of the mineral admixture, combining with the biochar and the waste incineration bottom ash and using cement as a bonding agent. The aggregate prepared by the preparation method completely meets various performance requirements of the high-strength light coarse aggregate, can replace natural light aggregate (pumice, shale and the like) and sintered light aggregate (steel slag powder sintered aggregate, ceramsite and the like) to be used as a raw material of light aggregate concrete, reduces the exploitation of the natural light aggregate on one hand, and can effectively save resources; on the other hand, compared with the energy consumed by sintering the ceramsite at thousands of ℃ in the prior art, the aggregate is prepared by a cold bonding method, so that the method is extremely low in energy consumption and pollution, and has great advantages in the aspects of energy conservation, environmental protection and the like. The invention provides a novel production method of carbon capture aggregate with high economic benefit and environmental protection benefit, which simultaneously realizes the improvement of the mechanical property of the aggregate, the capture and the sealing of carbon dioxide and the effective treatment of waste incineration bottom ash, protects the environment and saves resources.|[0078] It is to be understood that the invention is not limited to the examples described above, but that modifications and variations may be effected thereto by those of ordinary skill in the art in light of the foregoing description, and that all such modifications and variations are intended to be within the scope of the invention as defined by the appended claims. (CN114716200)|TECHNICAL FIELD|[0001] The invention relates to the technical field of concrete, in particular to carbon capture aggregate taking biochar and bottom ash as raw materials and a preparation method thereof.|BACKGROUND ART|[0002] The aggregate is a basic raw material for preparing concrete, approximately accounts for two thirds of the total mass of the concrete, and the demand of the aggregate is gradually increased along with the rapid increase of the annual use amount of the concrete. The existing aggregate is generally natural aggregate, such as pebbles, broken stones, river sand and the like, but with the over-mining of mines, rivers and the like, the natural resource of the aggregate is increasingly deficient, so that the use cost of the natural aggregate is increased. Therefore, it is of great importance to find artificial aggregates that can replace natural sands.|[0003] At present, due to the increase of the emission amount of carbon dioxide, global warming is increasingly serious, and the problems of severe drought, rainfall mode change, extreme heat waves, glacier melting, sea level rising and the like occur. The construction industry is one of the industries with serious carbon dioxide emission, and the total emission of the cement industry is estimated to account for nearly 8% of the global carbon dioxide emission.|[0004] The urban garbage is increased along with the continuous promotion of the urbanization process, and about 80 percent of the residual ash slag after the garbage is burnt is bottom ash, and 20 percent of the residual ash slag is fly ash. At present, the main treatment mode of the waste incineration bottom ash is landfill, but the landfill needs to occupy a large amount of land resources; and because the composition of the incineration waste is complex, the bottom ash may contain various heavy metals and inorganic salt substances, and in the landfill or utilization process of the waste incineration bottom ash, harmful components may be leached out under the action of factors such as acid rain and the like, so that the land environment is polluted.|[0005] Therefore, it is necessary to provide a carbon dioxide capture and sequestration technology to reduce the concentration of carbon dioxide in the atmosphere, and to find a reasonable waste incineration bottom ash disposal method to reduce the environmental problems such as land pollution and global warming, and to make the waste resources available for reuse.|DISCLOSURE|Disclosure of Invention|[0006] In view of the defects of the prior art, the invention aims to provide a carbon capturing aggregate using biochar and bottom ash as raw materials and a preparation method thereof, and aims to replace natural aggregate with high-strength light coarse carbon capturing aggregate prepared from biochar and waste incineration bottom ash as raw materials for preparing concrete, and simultaneously realize the improvement of the mechanical property of the aggregate, the capture and the sealing of carbon dioxide and the effective treatment of the waste incineration bottom ash, protect the environment and save resources.|[0007] The technical scheme of the invention is as follows:|[0008] in a first aspect of the present invention, there is provided a method for preparing a carbon-capturing aggregate using biochar and bottom ash as raw materials, comprising the steps of:|[0009] providing a waste biomass raw material, and pyrolyzing the waste biomass raw material to obtain charcoal ash particles;|[0010] providing waste incineration bottom ash, and naturally weathering and air-drying the waste incineration bottom ash to obtain waste incineration bottom ash particles;|[0011] mixing the biochar ash particles, the waste incineration bottom ash particles, cement and a mineral admixture according to the mass ratio of (0.1-0.5) to (7) to (1.5-1.9) to obtain a mixture;|[0012] and carrying out cold bonding granulation and maintenance on the mixture to obtain the carbon capture aggregate.|[0013] Optionally, the waste biomass feedstock comprises at least one of waste wood chips, crop residues, biological manure.|[0014] Optionally, the step of providing the waste biomass raw material and obtaining the biochar ash particles after pyrolysis specifically includes: providing a waste biomass raw material, grinding and screening the waste biomass raw material to ensure that the particle size of the waste biomass raw material is 0.063-2 mm, and obtaining biochar ash particles after pyrolysis.|[0015] Optionally, the pyrolysis temperature is 500-700 ℃ and the time is 2h.|[0016] Optionally, the particle size of the biochar ash particles is less than 2.36mm, and the particle size of the waste incineration bottom ash particles is less than 2.36mm.|[0017] Optionally, the specific steps of providing the waste incineration bottom ash, and obtaining the waste incineration bottom ash particles after natural weathering and air drying include:|[0018] providing waste incineration bottom ash, carrying out magnetic separation, naturally weathering and air drying for 28-35 days, crushing, and screening to obtain waste incineration bottom ash particles.|[0019] Optionally, the cement is portland cement.|[0020] Optionally, the step of obtaining the carbon capturing aggregate after cold bonding, granulation and curing of the mixture specifically includes:|[0021] putting the mixture into a disc granulator for cold bonding granulation to obtain a coarse aggregate blank body, wherein the particle size range of the coarse aggregate blank body is 4.75-16 mm;|[0022] and curing the coarse aggregate blank for at least 28 days under the conditions that the temperature is 20 +/-2 ℃ and the relative humidity is more than 95 percent to obtain the carbon capture aggregate.|[0023] Optionally, the inclination angle of the disc granulator is 45-60 degrees, the diameter of the disc is 1m, the edge height is 1.5cm, and the rotating speed is 35-55 rpm.|[0024] In a second aspect of the present invention, there is provided a carbon capturing aggregate using biochar and bottom ash as raw materials, wherein the carbon capturing aggregate is prepared by the above-described preparation method of the present invention.|[0025] Has the advantages that: the invention provides a preparation method of carbon capturing aggregate by taking biochar and bottom ash as raw materials, wherein biochar is added into the aggregate instead of part of cementing materials, so that the carbon capturing capability of the aggregate can be enhanced, the carbon dioxide emission in the hydration process of the aggregate is reduced, and the carbon fixing capability of the aggregate is enhanced; the high adsorption capacity of the biochar on organic and inorganic pollutants in the waste incineration bottom ash can greatly treat and stabilize the waste incineration bottom ash, and reduce the environmental pollution and the land resource use pressure; meanwhile, the biochar can promote the hydration of cement and the formation of hydration products through the internal curing effect, and generate an internal and external synergistic effect through external carbonization curing to enhance the carbonization degree, so that the mechanical property and the mechanical strength of the aggregate are enhanced. By utilizing the characteristics of porous and light biological carbon and waste incineration bottom ash particles, the prepared aggregate has lighter mass and can be used as light coarse aggregate. The mineral admixture is hydrated with cement to form hydration products such as C-S-H gel, ettringite and the like, so that heavy metals such as Cu, pb, cr and the like in bottom ash and inorganic salts can be well fixed, and the cement bottom ash is green and environment-friendly. The prepared aggregate has high strength and low water absorption rate by utilizing the characteristic of high activity of the volcanic ash of the mineral admixture, combining with the biochar and the waste incineration bottom ash and using cement as a bonding agent. The aggregate prepared by the preparation method completely meets various performance requirements of the high-strength light coarse aggregate, can replace natural light aggregate (pumice, shale and the like) and sintered light aggregate (steel slag powder sintered aggregate, ceramsite and the like) to be used as a raw material of light aggregate concrete, reduces the exploitation of the natural light aggregate on one hand, and can effectively save resources; on the other hand, compared with the energy consumed by sintering the ceramsite at thousands of ℃ in the prior art, the aggregate is prepared by a cold bonding method, so that the method is extremely low in energy consumption and pollution, and has great advantages in the aspects of energy conservation, environmental protection and the like. The invention provides a novel production method of carbon capture aggregate with high economic benefit and environmental protection benefit, which simultaneously realizes the improvement of the mechanical property of the aggregate, the capture and the sealing of carbon dioxide and the effective treatment of waste incineration bottom ash, protects the environment and saves resources.|DRAWINGS DESCRIPTION|[0026] FIG. 1 is a schematic flow chart of a method for preparing carbon-capturing aggregate from biochar and bottom ash according to an embodiment of the present invention.|INVENTION MODE|Detailed Description|[0027] The present invention provides a carbon capturing aggregate using biochar and bottom ash as raw materials and a method for preparing the same, and the present invention is further described in detail below in order to make the objects, technical solutions, and effects of the present invention clearer and clearer. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.|[0028] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.|[0029] The embodiment of the invention provides a preparation method of carbon capture aggregate by taking biochar and bottom ash as raw materials, as shown in figure 1, comprising the following steps:|[0030] s1, providing a waste biomass raw material, and pyrolyzing the waste biomass raw material to obtain charcoal ash particles;|[0031] s2, providing waste incineration bottom ash, and naturally weathering and air-drying the waste incineration bottom ash to obtain waste incineration bottom ash particles;|[0032] s3, mixing the biochar ash particles, the garbage incineration bottom ash particles, cement and mineral admixtures according to the ratio of (0.1-0.5): 7:1: (1.5-1.9) to obtain a mixture;|[0033] and S4, carrying out cold bonding granulation and maintenance on the mixture to obtain the carbon capture aggregate.|[0034] According to the invention, the biochar is added into the aggregate instead of part of cementing materials, so that the carbon capture capacity of the aggregate can be enhanced, the carbon dioxide emission in the aggregate hydration process is reduced, and the carbon fixation capacity of the aggregate is enhanced; the biochar has a mesoporous structure, relatively high surface area and rich functional groups, so that organic and inorganic pollutants in the waste incineration bottom ash can be adsorbed and fixed, and the waste incineration bottom ash can be treated and stabilized in a large amount, so that the aggregate has lighter weight, and the environmental pollution caused by the waste incineration bottom ash and the land resource use pressure caused by landfill of the waste incineration bottom ash are reduced; meanwhile, the biochar can promote the hydration of cement and the formation of hydration products through the internal curing effect (specifically, the porous structure of the biochar can adsorb water inside pores, and then the solidification is promoted and the hydration is improved through releasing water and increasing the internal relative humidity in the curing process, so that the hydration speed of the cement is increased, the hydration degree is improved), and the internal and external synergistic effect is generated through the external carbonization and curing, so that the carbonization degree is enhanced, and the mechanical property and the mechanical strength of the aggregate are enhanced. By utilizing the characteristics of porous and light weight of the biochar and waste incineration bottom ash particles, the prepared aggregate has lighter weight and can be used as light coarse aggregate. Hydration products such as C-S-H gel, ettringite and the like formed by hydration of the mineral admixture and cement can well fix heavy metals such as Cu, pb, cr and the like and inorganic salts in bottom ash, and the cement is green and environment-friendly. The aggregate prepared by utilizing the characteristic of strong activity of the mineral admixture volcanic ash, combining the mineral admixture with biochar and waste incineration bottom ash and adopting the cold bonding granulation technology through taking cement as a bonding agent has higher strength and lower water absorption. The aggregate prepared by the preparation method completely meets various performance requirements of the high-strength light coarse aggregate, and can replace natural light aggregates (pumice, shale and the like) and sintered light aggregates (steel slag powder sintered aggregates, ceramsite and the like) as the raw materials of the light aggregate concrete.|[0035] In step S1, in one embodiment, the waste biomass material includes at least one of waste wood chips, crop residues, and biological manure, but is not limited thereto. The biochar prepared from the waste biomass raw materials has a mesoporous structure, a relatively large surface area and rich functional groups, can adsorb and fix organic and inorganic pollutants in waste incineration bottom ash, can treat and stabilize the waste incineration bottom ash in a large amount, enables the aggregate to be lighter in weight, can adsorb water inside pores, and promotes solidification and improves hydration by releasing water and increasing internal relative humidity in a curing process, so that the cement hydration speed is increased, and the hydration degree is improved.|[0036] In one embodiment, the step of providing the waste biomass feedstock and obtaining the biochar ash particles after pyrolysis specifically comprises: providing a waste biomass raw material, grinding and screening the waste biomass raw material to ensure that the particle size of the waste biomass raw material is 0.063-2 mm, and pyrolyzing the waste biomass raw material to obtain the biochar ash particles. The use of finer biomass feedstock can increase the productivity of the biochar ash particles.|[0037] In one embodiment, the pyrolysis temperature is 500 to 700 ℃ and the time is 2 hours. The pyrolysis temperature is not too high or too low, and the pores of the biochar ash particles are too large due to too high temperature, so that the strength of the aggregate is influenced; too low a temperature results in a reduction in the carbon dioxide adsorption capacity of the biochar ash particles. Pyrolysis at a temperature in the range of 500 ℃ to 700 ℃ is the most suitable temperature for the biochar ash particles as an aggregate admixture. Specifically, the waste biomass raw material is placed in a muffle furnace, and the temperature is raised to 500-700 ℃ at a heating rate of 10 ℃/min and is kept for 2h. Preferably, the temperature of the pyrolysis is 600 ℃.|[0038] In specific implementation, the prepared charcoal ash particles are soaked in water at 100 ℃ for 0.5 hour until the charcoal ash particles are completely saturated, then vacuum drying and filtering are carried out to obtain saturated surface drying conditions, and then the charcoal ash particles are put into a transparent plastic bag to be sealed and stored for later use.|[0039] In one embodiment, the biochar ash particles have a particle size of less than 2.36mm to make them suitable for cold-bond pelletizing.|[0040] In step S2, in an embodiment, the specific steps of providing the waste incineration bottom ash, and obtaining the waste incineration bottom ash particles through natural weathering and air drying include:|[0041] providing waste incineration bottom ash, carrying out magnetic separation, naturally weathering and air drying for 28-35 days, crushing and screening to obtain waste incineration bottom ash particles. The waste incineration bottom ash is complex in raw material source and may contain a plurality of heavy metal elements, so that the metal in the bottom ash can be recycled through magnetic separation, and the next step of crushing is facilitated. The process can be used for specifically placing the waste incineration bottom ash on a conveyor belt of a magnetic separator, and then starting the magnetic separator for automatic magnetic separation. The natural weathering and the air drying are carried out simultaneously, the aim is to reduce the heavy metal in the bottom ash of the waste incineration, and the natural weathering and the air drying can be carried out in an outdoor and rainproof environment. Preferably, the natural weathering and air drying time is 30 days.|[0042] In one embodiment, the particle size of the waste incineration bottom ash particles is less than 2.36mm. The bottom ash with larger particle size can be directly used as a coarse aggregate to be applied to engineering, while the particles smaller than 2.36mm are difficult to treat, and the part accounts for more than 50 percent of the total amount of the bottom ash. In addition, the cold bonding technique is only suitable for the treatment of fine particulate matter, so bottom ash particles with a particle size of less than 2.36mm are selected.|[0043] In the step S3, the biochar ash particles, the waste incineration bottom ash particles, the cement and the mineral admixture are mixed according to the proportion of (0.1-0.5): 7:1: (1.5-1.9) to obtain a mixture. Too high a content of biochar ash particles leads to too high a porosity and a reduction in the mechanical strength of the aggregate. Under the proportion, the prepared aggregate has high production efficiency, uniform particle size distribution and high strength; moreover, the carbon dioxide adsorption capacity of the biochar can be stably exerted, and simultaneously, a large amount of waste incineration bottom ash can be treated, so that the economic cost is reduced, and the pollution to the environment caused by treating the waste incineration bottom ash is reduced. Preferably, the biochar ash particles, the waste incineration bottom ash particles, the cement and the mineral admixture are mixed according to the mass ratio of 0.3.|[0044] In one embodiment, the mineral admixture is preferably mineral fines. The reason is that the mineral powder has higher activity, and can well enhance the strength of the aggregate and reduce the water absorption of the aggregate.|[0045] In one embodiment, the cement is portland cement, but is not limited thereto. The main mineral compositions of portland cement are: tricalcium silicate, dicalcium silicate, tricalcium aluminate, tetracalcium aluminoferrite. Tricalcium silicate determines the strength of portland cement within four weeks; the strength of the dicalcium silicate is exerted after four weeks, and the strength of the dicalcium silicate reaches four weeks about one year; tricalcium aluminate develops strength faster but has lower strength, and plays a certain role in the strength of portland cement within 1 to 3 days or a little longer time; tetracalcium aluminoferrite also develops strength quickly, but has low strength and contributes little to the strength of portland cement.|[0046] In step S4, granulation is performed by adopting a cold bonding granulation technology. The cold bonding granulation technology has the advantages of low energy consumption and less pollutant emission, and has great advantages compared with sintered ceramsite requiring thousands of degrees centigrade and the like. The cold bonding granulation technology can recycle solid wastes, reduce the carbon dioxide emission in the aggregate preparation process and the environmental burden brought by solid waste landfill, and the product can replace natural aggregates, thereby effectively saving natural resources. Therefore, the cold bonding technology is applied to the treatment of the biochar and the municipal refuse incineration bottom ash, the biochar and the municipal refuse incineration bottom ash can be made into aggregate to be applied to concrete, the waste utilization can be realized, and the environmental pollution and the occupation of land resources are reduced.|[0047] In one embodiment, the step of obtaining the carbon capturing aggregate after cold binding granulation and curing of the mixture specifically comprises:|[0048] s41, putting the mixture into a disc granulator for cold bonding granulation to obtain a coarse aggregate blank body, wherein the particle size range of the coarse aggregate blank body is 4.75-16 mm;|[0049] s42, curing the coarse aggregate blank for at least 28 days at the temperature of 20 +/-2 ℃ and the relative humidity of more than 95% to obtain the carbon capture aggregate.|[0050] In step S41,4.75mm is the defined particle size of the coarse aggregate, and aggregates larger than 4.75mm are generally considered to be coarse aggregates. Further, since the aggregate is artificial, the strength of the aggregate tends to be rather lowered as the particle diameter is larger, and the strength of the aggregate having a particle diameter of more than 16mm is remarkably lowered. Therefore, the particle size range of the coarse aggregate blank is selected to be 4.75-16mm.|[0051] In specific implementation, the mixture is put into a disc granulator for stirring, water is uniformly sprayed on the mixture in the stirring process, the mass ratio of the total water consumption to the mixture is 20% -22% (when the ratio of the water to the mixture is too high or too low, the molding of the aggregate is greatly influenced, so that a proper aggregate cannot be produced or the granulation efficiency is low), and the proper rotation speed is kept, so that the mixture is fully polymerized under the action of moisture and centrifugation, and finally a coarse aggregate blank is obtained. In order to fully mix the raw materials, powdery materials such as biochar, waste incineration bottom ash and the like are put on a disc and stirred for about 5-10 minutes until the color is uniform and no obvious particles exist. In specific implementation, a part of the mixture is required to be reserved before the mixture is put into the disc granulator, and the mixture is added according to the proportion of the dry and wet conditions of the mixture in the subsequent water adding and mixing process. The final aggregate productivity and particle uniformity can be effectively improved by batch charging.|[0052] In one embodiment, the disk pelletizer has a disk inclination of 45 to 60 °, a disk diameter of 1m, a rim height of 1.5cm, and a rotational speed of 35 to 55rpm.|[0053] In step S42, the concrete can be maintained in water bath at different temperatures (20-80 ℃). The water bath maintenance can provide sufficient water, so that the internal hydration of the aggregate is sufficient, and the performance of the aggregate can be obviously enhanced. Wherein, the temperature is not suitable to be too high or too low; high temperature can cause the moisture of the aggregate to evaporate, and the performance of the aggregate is reduced; low temperatures can inhibit hydration, which in turn affects aggregate performance.|[0054] The embodiment of the invention also provides a carbon capturing aggregate which takes the biochar and the bottom ash as raw materials, wherein the carbon capturing aggregate is prepared by the preparation method disclosed by the embodiment of the invention. The single-particle compressive strength of the carbon capturing aggregate is 2.44-2.70 MPa, the carbon dioxide adsorption performance is 6.4-7.6 mmol/g, and the water absorption rate is 14.25-16.32%. According to the specification of GB T17431.1-lightweight aggregate and test method part 1 thereof, the carbon-capturing aggregate can be considered as lightweight aggregate, and according to the specification, the cylinder pressure strength of the aggregate meets the requirements of high-strength lightweight coarse aggregate. Compared with most commercial light coarse aggregates on the market, the aggregate prepared by the invention has higher strength and better performance; the water absorption rate is low, and the requirements of subsequent products can be met; the method has extremely high economic benefit and environmental protection benefit, and the biomass waste and the waste incineration bottom ash are recycled, so that the material cost is reduced and the environmental pollution is reduced; meanwhile, the aggregate is prepared by a cold bonding method, so that the energy consumption is extremely low, the pollution is less, and the method has great advantages compared with sintered ceramsite requiring thousands of degrees centigrade and the like.|[0055] The invention is further illustrated by the following specific examples.|[0056] In the following examples, the biochar ash particles used in the raw material were prepared by high temperature pyrolysis using waste wood chips with a particle size ranging from 0.063mm to 2mm as the raw material; the waste incineration bottom ash is the bottom ash produced by a waste incineration power plant, and bottom ash particles with the size smaller than 2.36mm are selected after magnetic separation, natural weathering and air drying; other raw materials, such as mineral admixture (selected from mineral powder or steel slag powder) and portland cement, are commercially available. The starting material compound composition is shown in table 1:|[0057] table 1: composition of raw Material Compounds|[0058] |[0059] Example 1:|[0060] sieving the waste wood chips to obtain the waste wood chips with the particle size of 0.063 mm-2 mm, then putting the waste wood chips into a muffle furnace for high-temperature pyrolysis at the heating rate of 10 ℃/min, keeping the temperature for two hours after the temperature is raised to 600 ℃ to obtain charcoal ash particles, soaking the charcoal ash particles in water with the temperature of 100 ℃ after cooling for 0.5 hour, then completely saturating the charcoal ash particles, and then drying the charcoal ash particles through vacuum filtration to obtain saturated surface drying conditions;|[0061] carry out moist cooling treatment after carrying out the magnetic separation from the remaining end ash after the incineration electricity generation that the msw incineration power plant was collected through the magnet separator, put it 1 natural month of morals and air-dry under natural condition again, then carry out screening: under the condition of 20 +/-2 ℃ of experimental environment, bottom ash passes through standard sieves of 37.5mm, 31.5mm, 26.5mm, 19mm, 16mm, 9.5mm, 4.75mm and 2.36mm, bottom ash (the content of the bottom ash accounts for more than 50 percent of the total volume) below 2.36mm is selected, and the rest of the bottom ash is crushed to 2.36mm after magnetic separation. Mixing biochar ash particles, mineral powder, portland cement and waste incineration bottom ash in a proportion of 0.1:1.9:1:7, fully mixing in a mass ratio;|[0062] the mixed raw materials are put into a disc granulator for granulation to obtain a light coarse aggregate blank body with the thickness of 4.75-16 mm;|[0063] and placing the granulated light coarse aggregate blank in an environment with the temperature of 20 +/-2 ℃ and the relative humidity of 95% for curing for 28 days to obtain the high-strength carbon capture aggregate.|[0064] Through tests, the single-particle compressive strength of the obtained carbon capture aggregate is 2.47MPa, the water absorption is 15.43%, and the carbon dioxide adsorption performance is 6.4mmol/g.|[0065] Example 2:|[0066] sieving the waste wood scraps to obtain the waste wood scraps with the grain size of 0.063 mm-2 mm, then putting the waste wood scraps into a muffle furnace for high-temperature pyrolysis at the heating rate of 10 ℃/min, keeping the temperature for two hours after the temperature is raised to 600 ℃ to obtain biochar ash particles, soaking the biochar ash particles in 100 ℃ water for 0.5 hour after cooling, fully saturating the biochar ash particles, and then drying the biochar ash particles through vacuum filtration to obtain saturated surface drying conditions.|[0067] Carry out moist cooling treatment after carrying out the magnetic separation from the remaining end ash after the incineration power generation that the msw incineration power plant was collected through the magnet separator, put it 1 natural month of morals and air-dry under natural condition again, then sieve and handle: under the condition of 20 +/-2 ℃ of experimental environment, bottom ash passes through standard sieves of 37.5mm, 31.5mm, 26.5mm, 19mm, 16mm, 9.5mm, 4.75mm and 2.36mm, bottom ash (the content of the bottom ash accounts for more than 50 percent of the total volume) below 2.36mm is selected, and the rest of the bottom ash is crushed to 2.36mm after magnetic separation. Mixing biochar ash particles, steel slag powder, portland cement and waste incineration bottom ash in a proportion of 0.3:1.7:1:7, fully mixing in a mass ratio;|[0068] the mixed raw materials are put into a disc granulator for granulation to obtain a light coarse aggregate blank body with the thickness of 4.75-16 mm;|[0069] and placing the granulated light coarse aggregate blank in an environment with the temperature of 20 +/-2 ℃ and the relative humidity of 95% for curing for 28 days to obtain the high-strength carbon capture aggregate.|[0070] Tests show that the compressive strength of the single particle of the obtained carbon capture aggregate is 2.70MPa, the water absorption rate is 16.32 percent, and the carbon dioxide adsorption performance is 7.3mmol/g.|[0071] Example 3:|[0072] sieving the waste wood scraps to obtain waste wood scraps with the particle size of 0.063 mm-2 mm, putting the waste wood scraps into a muffle furnace for high-temperature pyrolysis at the heating rate of 10 ℃/min, keeping the temperature for two hours after the temperature is raised to 600 ℃ to obtain biochar ash particles, cooling, soaking the biochar ash particles in 100 ℃ water for 0.5 hour, fully saturating, and then filtering and drying in vacuum to obtain saturated surface drying conditions;|[0073] carry out moist cooling treatment after carrying out the magnetic separation from the remaining end ash after the incineration electricity generation that the msw incineration power plant was collected through the magnet separator, put it 1 natural month of morals and air-dry under natural condition again, then carry out screening: under the condition of 20 +/-2 ℃ of experimental environment, bottom ash passes through standard sieves of 37.5mm, 31.5mm, 26.5mm, 19mm, 16mm, 9.5mm, 4.75mm and 2.36mm, bottom ash (the content of the bottom ash accounts for more than 50 percent of the total volume) below 2.36mm is selected, and the rest of the bottom ash is crushed to 2.36mm after magnetic separation. Mixing biochar ash particles, mineral powder, portland cement and waste incineration bottom ash in a proportion of 0.5:1.5:1:7, fully mixing in a mass ratio;|[0074] putting the mixed raw materials into a disc granulator for granulation to obtain a light coarse aggregate blank body with the thickness of 4.75-16 mm;|[0075] and placing the granulated light coarse aggregate blank in an environment with the temperature of 20 +/-2 ℃ and the relative humidity of 95% for curing for 28 days to obtain the high-strength carbon capture aggregate.|[0076] Tests show that the compressive strength of the single particle of the obtained carbon capture aggregate is 2.44MPa, the water absorption is 14.25 percent, and the carbon dioxide adsorption performance is 7.6mmol/g.|[0077] In conclusion, the invention provides a preparation method of carbon capturing aggregate by taking biochar and bottom ash as raw materials, and the biochar is added into the aggregate instead of part of cementing materials, so that the carbon capturing capability of the aggregate can be enhanced, the carbon dioxide emission in the hydration process of the aggregate is reduced, and the carbon fixing capability of the aggregate is enhanced; the high adsorption capacity of the biochar on organic and inorganic pollutants in the waste incineration bottom ash can greatly treat and stabilize the waste incineration bottom ash, and reduce the environmental pollution and the land resource use pressure; meanwhile, the biochar can promote cement hydration and improve the formation of hydration products through the internal curing effect, and the internal and external synergistic effect is generated through external carbonization curing to enhance the carbonization degree, so that the mechanical property and the mechanical strength of the aggregate are enhanced. By utilizing the characteristics of porous and light biological carbon and waste incineration bottom ash particles, the prepared aggregate has lighter mass and can be used as light coarse aggregate. The mineral admixture is hydrated with cement to form hydration products such as C-S-H gel, ettringite and the like, so that heavy metals such as Cu, pb, cr and the like in bottom ash and inorganic salts can be well fixed, and the cement bottom ash is green and environment-friendly. The prepared aggregate has high strength and low water absorption rate by utilizing the characteristic of high activity of the volcanic ash of the mineral admixture, combining with the biochar and the waste incineration bottom ash and using cement as a bonding agent. The aggregate prepared by the preparation method completely meets various performance requirements of the high-strength light coarse aggregate, can replace natural light aggregate (pumice, shale and the like) and sintered light aggregate (steel slag powder sintered aggregate, ceramsite and the like) to be used as a raw material of light aggregate concrete, reduces the exploitation of the natural light aggregate on one hand, and can effectively save resources; on the other hand, compared with the energy consumed by sintering the ceramsite at thousands of ℃ in the prior art, the aggregate is prepared by a cold bonding method, so that the method is extremely low in energy consumption and pollution, and has great advantages in the aspects of energy conservation, environmental protection and the like. The invention provides a novel production method of carbon capture aggregate with high economic benefit and environmental protection benefit, which simultaneously realizes the improvement of the mechanical property of the aggregate, the capture and the sealing of carbon dioxide and the effective treatment of waste incineration bottom ash, protects the environment and saves resources.|[0078] It is to be understood that the invention is not limited to the examples described above, but that modifications and variations may be effected thereto by those of ordinary skill in the art in light of the foregoing description, and that all such modifications and variations are intended to be within the scope of the invention as defined by the appended claims. Family Number|(100801613)|100801613|Abstract|(CN114716200B B)|The invention discloses a carbon capture aggregate with biochar and bottom ash as raw materials and a preparation method thereof . The preparation method comprises the steps that waste biomass raw materials are provided , and biochar ash particles are obtained after pyrolysis ; waste incineration bottom ash is provided , and waste incineration bottom ash particles are obtained after natural weathering and air drying ; mixing the charcoal ash particles , the waste incineration bottom ash particles , cement and a mineral admixture according to a mass ratio of ( 0.1-0.5 ) : 7 : 1 : ( 1.5-1.9 ) to obtain a mixture ; and carrying out cold bonding granulation on the mixture , and curing to obtain the carbon capture aggregate . The charcoal is added into the aggregate , so that emission of carbon dioxide in the hydration process can be reduced , and the carbon sequestration capacity of the aggregate is enhanced ; the biochar can promote cement hydration and formation of hydration products through an internal curing effect , and an internal and external synergistic effect is generated through external carbonization curing , so that the carbonization degree is enhanced , and the mechanical property and the mechanical strength of the aggregate are enhanced . |CPC codes|(CN114716200B B)|B01D - 053/62 |IPC codes|(CN114716200B B)|B01D - 053/62 | Environmental technology|Materials, metallurgy B01D-053/62|C04B-028/04|C04B-2111/00017|Y02W-030/91 (GR1) C04B-028/04[RK1]; C04B-018/10[RK2]; C04B-014/02/2[RK3]; C04B-018/12[RK4] B01D-053/62|C04B-028/04|C04B-2111/00017|Y02W-030/91 B01D-053/62|C04B-028/04 B01D-053/62|C04B-028/04 CN117923819|CN117658505|CN117285279|CN121407454B|CN119330625B|CN116409971B|CN115772007B|CN115925343B|CN115677306B|GB2623583;GB2623583 CN117923819 109522173 WHO=Examiner SELF=N CAT=A|CN117658505 108776076 WHO=Examiner SELF=N CAT=A|CN117285279 107901809 WHO=Examiner SELF=Y CAT=A|CN121407454B 117567434 WHO=Examiner SELF=N|CN119330625B 113118343 WHO=Examiner SELF=N|CN116409971B 105692796 WHO=Examiner SELF=Y|CN115772007B 104040520 WHO=Examiner SELF=N|CN115925343B 104465414 WHO=Examiner SELF=N|CN115677306B 103699095 WHO=Examiner SELF=Y|GB2623583 103603510 WHO=Examiner SELF=N CN113955738|CN113582569|CN110621634|CN107188478 CN113955738 98335874 WHO=Examiner SELF=N CAT=Y|CN113582569 96810024 WHO=Examiner SELF=Y CAT=Y|CN110621634 81910013 WHO=Examiner SELF=N CAT=Y|CN107188478 77331353 WHO=Examiner SELF=N CAT=A CN107188478; CN110621634; CN113582569; CN113955738 GRANTED (CN114716200)|GRANTED ALIVE (CN114716200)|ALIVE (CN114716200)|LEGAL DETAILS FOR CN114716200|Actual or expected expiration date=2042-03-07|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-03-07|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210223446|Application date=2022-03-07|Standardized application number=2022CN-0223446|Event publication date=2022-07-08|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114716200|Publication stage code=A|Publication date=2022-07-08|Standardized publication number=CN114716200|Event publication date=2022-07-08|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-07-26|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-02-03|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN114716200|Publication stage code=B|Publication date=2023-02-03|Standardized publication number=CN114716200B|Event publication date=2023-02-03|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN114716200)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTYHbP6NU5BRRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000066565856&ekey=2226&xpn=CN114716200B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=l2II8NKQdM2%252FBge6SRqprbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN114716200)|CN|(CN114716200)|CN (CN114716200)|NAME=SHENZHEN UNIVERSITY , COUNTRY=CN|(CN114716200)|NAME=SHENZHEN UNIVERSITY , COUNTRY=CN (CN114716200)|NAME=ZHU YANGBO;JOHNSON IP , REG=44268|(CN114716200)|NAME=ZHU YANGBO;JOHNSON IP , REG=44268 (CN114716200)|NAME=LIU JUN|NAME=LIU GUANG|NAME=XING FENG|NAME=LI ZHENLIN|(CN114716200)|NAME=LIU JUN|NAME=LIU GUANG|NAME=XING FENG|NAME=LI ZHENLIN 0 1 Titre: (CN114716200)|Carbon capture aggregate using biochar and bottom ash as raw materials and preparation method thereof Résumé: (CN114716200)|The invention discloses a carbon capture aggregate with biochar and bottom ash as raw materials and a preparation method thereof.The preparation method comprises the steps that waste biomass raw materials are provided, and biochar ash particles are obtained after pyrolysis; waste incineration bottom ash is provided, and waste incineration bottom ash particles are obtained after natural weathering and air drying; mixing the charcoal ash particles, the waste incineration bottom ash particles, cement and a mineral admixture according to a mass ratio of (0.1-0.5): 7: 1: (1.5-1.9) to obtain a mixture; and carrying out cold bonding granulation on the mixture, and curing to obtain the carbon capture aggregate. The charcoal is added into the aggregate, so that emission of carbon dioxide in the hydration process can be reduced, and the carbon sequestration capacity of the aggregate is enhanced; the biochar can promote cement hydration and formation of hydration products through an internal curing effect, and an internal and external synergistic effect is generated through external carbonization curing, so that the carbonization degree is enhanced, and the mechanical property and the mechanical strength of the aggregate are enhanced. 90 Abstract gpt-4o-mini no The article focuses on carbon capture using biochar and bottom ash in a construction context, which does not align with the topic of accelerated weathering for CO₂ sequestration.
90 CN201911324980 CN201911324980 CN110999751 88264022 CN110999751 A 2020-04-14 [CN110999751] 2019-12-20 2019-12-20 2020-04-14 (CN110999751)|2021-07-23 (CN110999751)|Biochar prepared from facility agriculture wastes, preparation method of biochar, soilless culture substrate and application of soilless culture substrate (CN110999751)|The invention provides a biochar prepared from facility agriculture wastes, a preparation method of the biochar, a soilless culture substrate and application of the soilless culture substrate, and belongs to the technical field of crop cultivation. The method for preparing the biochar from facility agriculture wastes comprises the following steps that the facility agriculture wastes are crushed and are then subjected to cracking for 3 to 4 h at 300 DEG C to 500 DEG C under the oxygen-free condition; and obtained cracking products are crushed to obtain the biochar. The prepared biochar containsrich porous structures and nutritional ingredients including rapidly available potassium, rapidly available phosphorus, rapidly available nitrogen, organic matters and salts; and the pH is alkaline,so that sufficient ventilation pores and nutrients are provided for crop growth. The invention also provides a vegetable soilless culture substrate containing the biochar. Compared with an existing soilless culture substrate, the vegetable soilless culture substrate provided by the invention has the advantages that the cucumber yield can be stably improved; the cyclic utilization of facility agriculture production wastes such as straws can also be realized; and carbon sequestration, emission reduction and green development are promoted. QINGDAO ACADEMY OF AGRICULTURAL SCIENCES (CN110999751)|QINGDAO ACADEMY OF AGRICULTURAL SCIENCES ([CN]) ZHANG GONGCHEN|WAN SHUWEI|ZHAO AIHONG|ZHANG SHOUCAI|LI LEI|QIN YUHONG|WANG BO|JIANG ZHIXUN|WANG ZHENQING|LIU LING|LI HAINING (CN110999751)|ZHANG GONGCHEN|WAN SHUWEI|ZHAO AIHONG|ZHANG SHOUCAI|LI LEI|QIN YUHONG|WANG BO|JIANG ZHIXUN|WANG ZHENQING|LIU LING|LI HAINING (CN110999751)|DONG DAYUAN;BEIJING GAOWO LAW FIRM|Reg. Nb: 11569 (CN110999751)|As the grass carbon in the matrix is difficult to regenerate resources, the production cost of the matrix is high, and particularly, the foreign excellent grass carbon has higher price and is difficult to utilize in production.|However, the treatment of facility agricultural wastes and waste vegetables in the current production is always a difficult problem in the facility production. At present, the treatment modes of the wastes mainly include concentrated composting, crushing and returning to the field, garbage treatment, incineration and the like, wherein the compost is placed in the waste treatment device, and the compost takes a certain land space due to long treatment time, so that the waste treatment device is difficult to popularize in production.|The method not only solves the problem that agricultural wastes are difficult to treat, but also provides a raw material source for the soilless culture substrate.| (CN110999751)|1. The method for preparing the biochar by utilizing the facility agricultural wastes is characterized by comprising the following steps:and crushing the facility agricultural wastes, and then cracking for 3-4 h at 300-500 ℃ under an anaerobic condition, and crushing the obtained cracking product to obtain the biochar.| (CN110999751)|In view of the above, the present invention is directed to provide biochar prepared from facility agricultural wastes, which has rich nutrient content and excellent physicochemical properties, solves the problem of difficulty in treating agricultural wastes, and provides a part of raw material sources for soilless culture substrates, and a method for preparing the same The invention also provides a vegetable soilless culture substrate and application thereof, which not only can stably improve the vegetable planting yield, but also can realize the cyclic utilization of agricultural production wastes such as facility vegetable straws and the like, and promote the carbon fixation, emission reduction and green development. The invention provides a preparation method for preparing biochar by utilizing facility agricultural wastes, which comprises the following steps:|The invention provides biochar prepared by the preparation method, which comprises the following nutrients in parts by weight:|The invention provides biochar prepared from facility agricultural wastes, a preparation method thereof, a soilless culture substrate and application thereof, and belongs to the technical field of crop culture.| (CN110999751)|SOILLESS CULTURE SUBSTRATE(100,31)|BIOCHAR(100,22)|FACILITY(100,9)|SUBSTRATE(100,1)|CROP CULTURE(52,1)|FACILITY AGRICULTURAL WASTE(43,15)|VENTILATION PORE(42,1)|PLANTING VEGETABLE(34,1)|FACILITY AGRICULTURAL PRODUCTION RECYCLING(33,1)|ANAEROBIC CONDITION(31,5)|EGGPLANT STRAW(30,3)|CRACKING PRODUCT(28,7)|QUICK ACTING PHOSPHORUS(24,6)|TOMATO STRAW BIOCHAR(23,4)|CRACK(22,4)|PREPARED BIOCHAR(22,2)|NUTRIENT COMPONENT(21,1)|QUICK ACTING POTASSIUM(20,6)|VEGETABLE SOILLESS CULTURE SUBSTRATE(20,6)|QUICK ACTING NITROGEN(18,6)|PYROLYSIS TEMPERATURE(18,1)|BIOCHAR MASS RATIO(15,1)|SOILLESS CUCUMBER CULTIVATION(14,1)|TOTAL PHOSPHORUS(12,3)|RICH POROUS STRUCTURE(12,2)|HARVESTING COMMODITY MELON(12,1)|TOMATO SEEDLING BIOCHAR(12,1)|TOMATO STRAW INFLUENCE(11,2)|ADDING TOMATO STRAW GRAPH(10,2)|CARBON FIXATION(10,2)|SOILLESS CULTURE SUBSTRATE INFLUENCE(10,2)|FACILITY TOMATO STRAW(10,1)|ORGANIC MATTER(9,5)|TOTAL NITROGEN(9,4)|TOTAL POTASSIUM(9,4)|GREEN DEVELOPMENT(9,2)|CLEAVAGE PRODUCT(9,1)|FACILITY RECYCLABLE UTILIZATION(9,1)|SOILLESS CULTURE POT(9,1)|CRUSHED PARTICLE SIZE(8,2)|CUCUMBER STEM THICKNESS(8,2)|BIOCHAR DECREASED CUCUMBER YIELD(8,1)|EGGPLANT SEEDLING(8,1)|FUTURE FACILITY AGRICULTURE(8,1)|CUCUMBER THICKNESS(7,3)|CUCUMBER GROWTH(7,2)|EMISSION REDUCTION(7,2)|AGRICULTURAL CULTIVATION(7,1)|ALKALI DEDIFFUSION(7,1)|BIOCHAR NUTRIENT CONTENT(7,1)|CROP PLANTING(7,1)|CUCUMBER SEEDLING(7,1)|CULTURE NUTRIENT SOLUTION FERTILIZER(7,1)|PLANTING MANAGEMENT(7,1)|SOILLESS CULTURE GROOVE(7,1)|VEGETABLE CULTIVATION(7,1)|VEGETABLE SUBSTRATE CULTIVATION(7,1)|PH VALUE(6,5)|PERLITE(6,4)|CROP CULTIVATION(6,1)|FLAME PHOTOMETRY(6,1)|GARDEN TREE(6,1)|GREENHOUSE HUMIDITY(6,1)|PHOSPHORUS WARP(6,1)|SCIENTIFIC UTILIZATION(6,1)|SITTING MELON PERIOD(6,1)|SOIL BORNE DISEASE RISK(6,1)|WHEAT STRAW(6,1)|CRACKING RESIDUE(5,1)|FACILITY VEGETABLE PRODUCTION(5,1)|ILLUMINATION INTENSITY(5,1)|PEANUT SHELL(5,1)|TOXIC EXCITATION(5,1)|WATER CONTENT(4,3)|CRACKING TEMPERATURE(4,2)|PHYSICOCHEMICAL PROPERTY(4,2)|PRODUCING FACILITY(4,2)|ACETOXY ACID(4,1)|CO2THE(4,1)|CUMULATIVE YIELD(4,1)|FRUIT SETTING(4,1)|GRASS CARBON(4,1)|MATRIX CULTURE(4,1)|NUTRIENT CONTENT DETECTION(4,1)|RICH NUTRIENT COMPONENT(4,1)|SOILLESS CULTURE SUBSTRATE SOURCE(4,1)|TEMPERATURE CARBONIZATION FURNACE(4,1)|VEGETABLE YIELD(4,1)|CUCUMBER PLANT HEIGHT(3,3)|ANALYZER(3,1)|CONTAMINATION(3,1)|CRUSHER(3,1)|CULTIVATION AREA(3,1)| (CN110999751)|1. The method for preparing the biochar by utilizing the facility agricultural wastes is characterized by comprising the following steps:|and crushing the facility agricultural wastes, and then cracking for 3-4 h at 300-500 ℃ under an anaerobic condition, and crushing the obtained cracking product to obtain the biochar.|2. The method according to claim 1, wherein the water content of the facility agricultural waste is 10% to 15%.|3. A method of producing as claimed in claim 1 or claim 2 wherein the facility agricultural waste comprises tomato straw, pepper straw or eggplant straw.|4. The preparation method according to claim 1, wherein the pyrolysis temperature of the facility agricultural waste is 350-450 ℃.|5. The preparation method according to claim 1 or 4, wherein the facility agricultural waste is cracked for 3-4 hours.|6. The method according to any one of claims 1, 2 and 4, wherein the crushed particle size of the cleavage product is 1 to 2 mm.|7. The biochar prepared by the preparation method of any one of claims 1 to 6 is characterized by comprising the following nutrients:|154.0mg/kg of quick-acting nitrogen, 1240.0mg/kg of quick-acting phosphorus, 19.00g/kg of quick-acting potassium, 66.89g/kg of organic matters, 28.88g/kg of salt, 2.37 percent of total nitrogen, 1.72 percent of total phosphorus, 4.1 percent of total potassium and 9.23 of pH value.|8. A soilless culture substrate for vegetables, comprising the biochar of claim 7 and a soilless culture substrate; the mass ratio of the biochar to the soilless culture substrate is 1-3: 100.|9. The soilless culture substrate for vegetables in claim 8 is used for planting vegetables. (CN110999751)|TECHNICAL FIELD|[0002] The invention belongs to the technical field of crop cultivation, and particularly relates to biochar prepared from facility agricultural wastes, a preparation method of the biochar, a vegetable soilless culture substrate and application of the vegetable soilless culture substrate.|BACKGROUND ART|[0004] The facility vegetable production plays an important role in facility production in China, wherein the cultivation areas of tomatoes and cucumbers are respectively positioned at the first place and the second place. However, the treatment of facility agricultural wastes and waste vegetables in the current production is always a difficult problem in the facility production. At present, the treatment modes of the wastes mainly include concentrated composting, crushing and returning to the field, garbage treatment, incineration and the like, wherein the compost is placed in the waste treatment device, and the compost takes a certain land space due to long treatment time, so that the waste treatment device is difficult to popularize in production. And the second crop planting is influenced by crushing and returning to the field, so that diseases and insect pests exist, and the risk of soil-borne diseases is particularly increased. But also causes pollution to the environment as garbage disposal or incineration.|[0005] Scientific and recyclable utilization of facility agricultural wastes is imminent, biochar is a product formed by cracking the agricultural wastes under the condition of high temperature and limited oxygen, has the characteristics of high carbon content, porous structure, difficult degradation in soil and the like, and has wide application in soil improvement water and soil conservation and heavy metal adsorption. Therefore, the method has important significance on how to prepare wastes such as tomato seedlings, cucumber seedlings, eggplant seedlings and the like generated in facility production into biochar required by agricultural cultivation.|[0006] Soilless culture is an important form of future facility agriculture, at present, the soilless culture in China is mainly based on matrix culture and mainly prepared from turf, vermiculite and perlite according to a certain proportion. As the grass carbon in the matrix is difficult to regenerate resources, the production cost of the matrix is high, and particularly, the foreign excellent grass carbon has higher price and is difficult to utilize in production.|DISCLOSURE|[0007] Disclosure of Invention|[0008] In view of the above, the present invention is directed to provide biochar prepared from facility agricultural wastes, which has rich nutrient content and excellent physicochemical properties, solves the problem of difficulty in treating agricultural wastes, and provides a part of raw material sources for soilless culture substrates, and a method for preparing the same|[0009] The invention also provides a vegetable soilless culture substrate and application thereof, which not only can stably improve the vegetable planting yield, but also can realize the cyclic utilization of agricultural production wastes such as facility vegetable straws and the like, and promote the carbon fixation, emission reduction and green development.|[0010] The invention provides a preparation method for preparing biochar by utilizing facility agricultural wastes, which comprises the following steps:|[0011] and crushing the facility agricultural wastes, and then cracking for 3-4 h at 300-500 ℃ under an anaerobic condition, and crushing the obtained cracking product to obtain the biochar.|[0012] Preferably, the water content of the facility agricultural waste is 10% to 15%.|[0013] Preferably, the facility agricultural waste comprises tomato straw, pepper straw or eggplant straw.|[0014] Preferably, the cracking temperature of the facility agricultural waste is 350-450 ℃.|[0015] Preferably, the facility agricultural waste has a cracking time of 3.5 h.|[0016] Preferably, the crushing particle size of the cracking product is 1-2 mm.|[0017] The invention provides biochar prepared by the preparation method, which comprises the following nutrients in parts by weight:|[0018] 154.0mg/kg of quick-acting nitrogen, 1240.0mg/kg of quick-acting phosphorus, 19.00g/kg of quick-acting potassium, 66.89g/kg of organic matters, 28.88g/kg of salt, 2.37 percent of total nitrogen, 1.72 percent of total phosphorus, 4.1 percent of total potassium and 9.23 of pH value.|[0019] The invention provides a vegetable soilless culture substrate, which comprises biochar and a soilless culture substrate; the mass ratio of the biochar to the soilless culture substrate is 1-3: 100.|[0020] The invention provides an application of the soilless culture substrate for vegetables in vegetable planting.|[0021] The invention provides a method for preparing biochar by using facility agricultural wastes, which comprises the steps of crushing the facility agricultural wastes, then cracking the crushed wastes for 3-4 hours at 300-500 ℃ under an anaerobic condition, and crushing the obtained cracking products to obtain the biochar. The prepared biochar contains rich nutrient components including quick-acting potassium, quick-acting phosphorus and quick-acting nitrogen as well as organic matters and salt, and the pH value is alkaline, so that sufficient nutrients are provided for the growth of crops. Meanwhile, the biochar is subjected to pyrolysis in the preparation process, has a rich porous structure, and provides root oxygen for the growth of crops. The method not only solves the problem that agricultural wastes are difficult to treat, but also provides a raw material source for the soilless culture substrate.|[0022] Compared with the existing vegetable substrate cultivation method, the vegetable soilless culture substrate containing the biochar prepared by the scheme is used, the vegetable yield can be stably improved, agricultural production wastes such as straws can be recycled, and carbon fixation, emission reduction and green development are promoted.|DRAWINGS DESCRIPTION|[0024] FIG. 1 shows the influence of the addition of tomato straw biochar to a soilless culture substrate on the plant height and stem thickness of cucumber; wherein, fig. 1-A is a bar chart of the influence of the soilless culture substrate added with the tomato straw biochar on the plant height of the cucumber, and fig. 1-B is a bar chart of the influence of the soilless culture substrate added with the tomato straw biochar on the stem thickness of the cucumber;|[0025] fig. 2 is a graph of the effect of adding tomato straw biochar to a soilless culture substrate on the individual plant yield and the average per mu yield of cucumbers, wherein fig. 2-A is a bar graph of adding tomato straw biochar to the soilless culture substrate on the individual plant yield of cucumbers, and fig. 2-B is a bar graph of adding tomato straw biochar to the soilless culture substrate on the average per mu yield of cucumbers.|INVENTION MODE|[0026] Detailed Description|[0027] The invention provides a method for preparing biochar by utilizing facility agricultural wastes, which comprises the following steps:|[0028] and crushing the facility agricultural wastes, and then cracking for 3-4 h at 300-500 ℃ under an anaerobic condition, and crushing the obtained cracking product to obtain the biochar.|[0029] In the present invention, the facility agricultural waste includes all crop waste in agricultural production, preferably includes tomato straw, pepper straw or eggplant straw. The source of the facility agricultural waste is not particularly limited in the present invention, and the facility agricultural waste known in the art may be used. The facility agricultural waste is preferably dried prior to pyrolysis. The method of drying is not particularly limited in the present invention, and drying schemes well known in the art, such as natural drying or mechanical drying, may be used. The drying degree is such that the water content of the agricultural waste of facilities is preferably 10% to 15%, more preferably 11% to 14%, and still more preferably 12% to 13%.|[0030] In the invention, the cracking temperature of the facility agricultural waste is preferably 350-450 ℃, and most preferably 400 ℃. The cracking time of the facility agricultural waste is preferably 3.5 h. The pyrolysis is preferably carried out in a high temperature carbonization furnace.|[0031] In the invention, the crushed particle size of the cracking product is preferably 1-2 mm, and more preferably 1.5 mm. The biochar is prepared by adopting the scheme, and the yield is 25-30%.|[0032] The invention provides biochar prepared by the preparation method, which comprises the following nutrients in parts by weight:|[0033] 154.0mg/kg of quick-acting nitrogen, 1240.0mg/kg of quick-acting phosphorus, 19.00g/kg of quick-acting potassium, 66.89g/kg of organic matters, 28.88g/kg of salt, 2.37 percent of total nitrogen, 1.72 percent of total phosphorus, 4.1 percent of total potassium and 9.23 of pH value.|[0034] The invention provides a vegetable soilless culture substrate, which comprises biochar and a soilless culture substrate; the mass ratio of the biochar to the soilless culture substrate is 1-3: 100. The soilless culture substrate comprises grass carbon: vermiculite: perlite. The grass carbon: the volume ratio of the vermiculite to the perlite is 3:1: 1. The source of the soilless culture substrate is not particularly limited in the invention, and the soilless culture substrate known in the field can be used. The soilless culture substrate for vegetables preferably also comprises moisture. The addition amount of the water accounts for 50-60% of the total mass of the soilless culture substrate. According to the preparation method of the vegetable soilless culture substrate, the biochar and the soilless culture substrate are mixed in proportion.|[0035] The invention provides an application of the soilless culture substrate for vegetables in vegetable planting.|[0036] In the present invention, the method for vegetable cultivation preferably comprises the steps of:|[0037] and (3) loading the soilless culture substrate of the vegetables into a pot or a soilless culture groove, watering thoroughly, planting the vegetables after 1-2 days, and performing conventional planting management.|[0038] The following examples are provided to describe the biochar prepared by using agricultural wastes, the method for preparing the biochar, the soilless culture substrate for vegetables and the application of the soilless culture substrate for vegetables in the present invention in detail, but the scope of the present invention should not be construed as being limited thereto.|INVENTION MODE|[0039] Example 1|[0040] Preparation method of biochar|[0041] Utilizing agricultural wastes such as facility tomato straws, wheat straws, peanut shells, rice hulls, garden trees and the like to crack for 3-4 hours at 300-500 ℃ under an anaerobic condition, crushing a cracking product to 1-2 mm by using a crusher, detecting nutrient content and physicochemical properties, and determining the detection method by referring to a soil sample analysis method, namely a quick-acting nitrogen alkali de-diffusion method; the quick-acting potassium and the total potassium are measured by flame photometry; measuring the quick-acting phosphorus by an Olsen-molybdenum-antimony colorimetric method; organic substance adopts TOC, measuring by using an analyzer; the total nitrogen is measured by adopting a semi-micro Kjeldahl method; all phosphorus warp H2SO4-HClO4After digestion, measuring by a molybdenum-antimony colorimetric method; the pH value is water: diluting the mixture according to the carbon ratio of 5:1, and measuring the mixture by a pH meter; and (4) determining the content of the water-soluble total salt by adopting a residue drying-mass method. The results are shown in Table 1.|[0042] TABLE 1 content of biochar nutrients and physicochemical properties from different agricultural waste sources|[0043] |[0044] |INVENTION MODE|[0045] Example 2|[0046] The tomato straw biochar prepared in the example 1 is added into a soilless culture substrate to improve the cucumber yield|[0047] 1. The experiment was designed in a randomized block, with 3 treatments, each repeated 3 times. Adding the tomato straw biochar into a commercial soilless culture substrate according to the mass ratio of 0% (B0), 3% (B3) and 5% (B5) (the volume ratio of the turf to the vermiculite to the perlite is 3:1:1), fully mixing, and filling into soilless culture pots (the length, the width and the height of each pot are 76cm, 42cm and 27cm, and each pot contains 10kg of culture substrate) for later use.|[0048] 2. Transplanting 3-4 true leaves of south China type cucumber variety 'Yulong', watering the matrix thoroughly 2 days before planting, planting 2 plants in each pot, processing 16 plants for planting, and watering for planting once after planting. And managing after planting according to a conventional soilless cucumber cultivation method. Watering the soilless culture nutrient solution fertilizer once every 2 days in the seedling stage (the EC value is 1.6), and watering the nutrient solution fertilizer once every day in the flowering and fruit setting stage; the temperature in the greenhouse is controlled to be 25 ℃ on average in the daytime and 20 ℃ on average at night; greenhouse humidity, illumination intensity and CO2The concentration is not controlled and is consistent with the natural condition.|[0049] 3. Harvesting: planting in 2019, 9 and 15 days, harvesting in 10 and 22 days, finishing harvesting in 11 and 09 days, harvesting commodity melons every day or every other day in the sitting melon period, and expressing the yield of each plant according to the cumulative yield of a cell.|[0050] Test results|[0051] 1. Influence of tomato straw biochar added into soilless culture substrate on cucumber growth|[0052] The plant height and stem thickness of the cucumber are measured in the cucumber sitting-cucumber full-season. As shown in fig. 1-a and fig. 1-B, the plant height and stem thickness of the cucumber were not significantly different from those of the control treatment (adding biochar 0) by adding 3% of biochar to the soilless culture substrate, while the plant height of the cucumber was significantly reduced by adding 5% of biochar to the soilless culture substrate without significantly affecting the stem thickness of the cucumber. Under each treatment condition, cucumber plant height and stem thickness measured at 3% charcoal treatment were the greatest.|[0053] 2. Influence of tomato straw biochar added into soilless culture substrate on cucumber yield|[0054] As shown in fig. 2-a and 2-B, the addition of 3% of tomato straw biochar to the soilless culture substrate significantly increased cucumber yield, which was 22.8% higher than the control treatment (0 added with biochar), while the addition of 5% of biochar decreased cucumber yield, which was 8.57% lower than the control treatment. This is probably due to the fact that the high salt content in the tomato seedling biochar and the organic compounds thereof, such as n-alkanoic acid, hydroxy and acetoxy acid-containing compounds, benzoic acid and phenols, are easily re-condensed into the biochar during the waste cracking and cooling process, and the compounds have a promoting effect (toxic excitation effect) on the growth of crops under the condition of low concentration and are harmful to the growth of crops under the condition of high concentration. Therefore, it is presumed that the high content of organic compounds and high salt contained in the vegetable soilless culture substrate to which the 3% tomato straw biochar is added inhibits the growth of cucumber. Therefore, the amount of the tomato straw biochar added into the soilless culture substrate is not higher than 5%, and the yield increase effect of the cucumber is the best by adding 3% biochar in the experimental example.|[0055] The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention. (CN110999751)|TECHNICAL FIELD|[0002] The invention belongs to the technical field of crop cultivation, and particularly relates to biochar prepared from facility agricultural wastes, a preparation method of the biochar, a vegetable soilless culture substrate and application of the vegetable soilless culture substrate.|BACKGROUND ART|[0004] The facility vegetable production plays an important role in facility production in China, wherein the cultivation areas of tomatoes and cucumbers are respectively positioned at the first place and the second place. However, the treatment of facility agricultural wastes and waste vegetables in the current production is always a difficult problem in the facility production. At present, the treatment modes of the wastes mainly include concentrated composting, crushing and returning to the field, garbage treatment, incineration and the like, wherein the compost is placed in the waste treatment device, and the compost takes a certain land space due to long treatment time, so that the waste treatment device is difficult to popularize in production. And the second crop planting is influenced by crushing and returning to the field, so that diseases and insect pests exist, and the risk of soil-borne diseases is particularly increased. But also causes pollution to the environment as garbage disposal or incineration.|[0005] Scientific and recyclable utilization of facility agricultural wastes is imminent, biochar is a product formed by cracking the agricultural wastes under the condition of high temperature and limited oxygen, has the characteristics of high carbon content, porous structure, difficult degradation in soil and the like, and has wide application in soil improvement water and soil conservation and heavy metal adsorption. Therefore, the method has important significance on how to prepare wastes such as tomato seedlings, cucumber seedlings, eggplant seedlings and the like generated in facility production into biochar required by agricultural cultivation.|[0006] Soilless culture is an important form of future facility agriculture, at present, the soilless culture in China is mainly based on matrix culture and mainly prepared from turf, vermiculite and perlite according to a certain proportion. As the grass carbon in the matrix is difficult to regenerate resources, the production cost of the matrix is high, and particularly, the foreign excellent grass carbon has higher price and is difficult to utilize in production.|DISCLOSURE|[0007] Disclosure of Invention|[0008] In view of the above, the present invention is directed to provide biochar prepared from facility agricultural wastes, which has rich nutrient content and excellent physicochemical properties, solves the problem of difficulty in treating agricultural wastes, and provides a part of raw material sources for soilless culture substrates, and a method for preparing the same|[0009] The invention also provides a vegetable soilless culture substrate and application thereof, which not only can stably improve the vegetable planting yield, but also can realize the cyclic utilization of agricultural production wastes such as facility vegetable straws and the like, and promote the carbon fixation, emission reduction and green development.|[0010] The invention provides a preparation method for preparing biochar by utilizing facility agricultural wastes, which comprises the following steps:|[0011] and crushing the facility agricultural wastes, and then cracking for 3-4 h at 300-500 ℃ under an anaerobic condition, and crushing the obtained cracking product to obtain the biochar.|[0012] Preferably, the water content of the facility agricultural waste is 10% to 15%.|[0013] Preferably, the facility agricultural waste comprises tomato straw, pepper straw or eggplant straw.|[0014] Preferably, the cracking temperature of the facility agricultural waste is 350-450 ℃.|[0015] Preferably, the facility agricultural waste has a cracking time of 3.5 h.|[0016] Preferably, the crushing particle size of the cracking product is 1-2 mm.|[0017] The invention provides biochar prepared by the preparation method, which comprises the following nutrients in parts by weight:|[0018] 154.0mg/kg of quick-acting nitrogen, 1240.0mg/kg of quick-acting phosphorus, 19.00g/kg of quick-acting potassium, 66.89g/kg of organic matters, 28.88g/kg of salt, 2.37 percent of total nitrogen, 1.72 percent of total phosphorus, 4.1 percent of total potassium and 9.23 of pH value.|[0019] The invention provides a vegetable soilless culture substrate, which comprises biochar and a soilless culture substrate; the mass ratio of the biochar to the soilless culture substrate is 1-3: 100.|[0020] The invention provides an application of the soilless culture substrate for vegetables in vegetable planting.|[0021] The invention provides a method for preparing biochar by using facility agricultural wastes, which comprises the steps of crushing the facility agricultural wastes, then cracking the crushed wastes for 3-4 hours at 300-500 ℃ under an anaerobic condition, and crushing the obtained cracking products to obtain the biochar. The prepared biochar contains rich nutrient components including quick-acting potassium, quick-acting phosphorus and quick-acting nitrogen as well as organic matters and salt, and the pH value is alkaline, so that sufficient nutrients are provided for the growth of crops. Meanwhile, the biochar is subjected to pyrolysis in the preparation process, has a rich porous structure, and provides root oxygen for the growth of crops. The method not only solves the problem that agricultural wastes are difficult to treat, but also provides a raw material source for the soilless culture substrate.|[0022] Compared with the existing vegetable substrate cultivation method, the vegetable soilless culture substrate containing the biochar prepared by the scheme is used, the vegetable yield can be stably improved, agricultural production wastes such as straws can be recycled, and carbon fixation, emission reduction and green development are promoted.|DRAWINGS DESCRIPTION|[0024] FIG. 1 shows the influence of the addition of tomato straw biochar to a soilless culture substrate on the plant height and stem thickness of cucumber; wherein, fig. 1-A is a bar chart of the influence of the soilless culture substrate added with the tomato straw biochar on the plant height of the cucumber, and fig. 1-B is a bar chart of the influence of the soilless culture substrate added with the tomato straw biochar on the stem thickness of the cucumber;|[0025] fig. 2 is a graph of the effect of adding tomato straw biochar to a soilless culture substrate on the individual plant yield and the average per mu yield of cucumbers, wherein fig. 2-A is a bar graph of adding tomato straw biochar to the soilless culture substrate on the individual plant yield of cucumbers, and fig. 2-B is a bar graph of adding tomato straw biochar to the soilless culture substrate on the average per mu yield of cucumbers.|INVENTION MODE|[0026] Detailed Description|[0027] The invention provides a method for preparing biochar by utilizing facility agricultural wastes, which comprises the following steps:|[0028] and crushing the facility agricultural wastes, and then cracking for 3-4 h at 300-500 ℃ under an anaerobic condition, and crushing the obtained cracking product to obtain the biochar.|[0029] In the present invention, the facility agricultural waste includes all crop waste in agricultural production, preferably includes tomato straw, pepper straw or eggplant straw. The source of the facility agricultural waste is not particularly limited in the present invention, and the facility agricultural waste known in the art may be used. The facility agricultural waste is preferably dried prior to pyrolysis. The method of drying is not particularly limited in the present invention, and drying schemes well known in the art, such as natural drying or mechanical drying, may be used. The drying degree is such that the water content of the agricultural waste of facilities is preferably 10% to 15%, more preferably 11% to 14%, and still more preferably 12% to 13%.|[0030] In the invention, the cracking temperature of the facility agricultural waste is preferably 350-450 ℃, and most preferably 400 ℃. The cracking time of the facility agricultural waste is preferably 3.5 h. The pyrolysis is preferably carried out in a high temperature carbonization furnace.|[0031] In the invention, the crushed particle size of the cracking product is preferably 1-2 mm, and more preferably 1.5 mm. The biochar is prepared by adopting the scheme, and the yield is 25-30%.|[0032] The invention provides biochar prepared by the preparation method, which comprises the following nutrients in parts by weight:|[0033] 154.0mg/kg of quick-acting nitrogen, 1240.0mg/kg of quick-acting phosphorus, 19.00g/kg of quick-acting potassium, 66.89g/kg of organic matters, 28.88g/kg of salt, 2.37 percent of total nitrogen, 1.72 percent of total phosphorus, 4.1 percent of total potassium and 9.23 of pH value.|[0034] The invention provides a vegetable soilless culture substrate, which comprises biochar and a soilless culture substrate; the mass ratio of the biochar to the soilless culture substrate is 1-3: 100. The soilless culture substrate comprises grass carbon: vermiculite: perlite. The grass carbon: the volume ratio of the vermiculite to the perlite is 3:1: 1. The source of the soilless culture substrate is not particularly limited in the invention, and the soilless culture substrate known in the field can be used. The soilless culture substrate for vegetables preferably also comprises moisture. The addition amount of the water accounts for 50-60% of the total mass of the soilless culture substrate. According to the preparation method of the vegetable soilless culture substrate, the biochar and the soilless culture substrate are mixed in proportion.|[0035] The invention provides an application of the soilless culture substrate for vegetables in vegetable planting.|[0036] In the present invention, the method for vegetable cultivation preferably comprises the steps of:|[0037] and (3) loading the soilless culture substrate of the vegetables into a pot or a soilless culture groove, watering thoroughly, planting the vegetables after 1-2 days, and performing conventional planting management.|[0038] The following examples are provided to describe the biochar prepared by using agricultural wastes, the method for preparing the biochar, the soilless culture substrate for vegetables and the application of the soilless culture substrate for vegetables in the present invention in detail, but the scope of the present invention should not be construed as being limited thereto.|INVENTION MODE|[0039] Example 1|[0040] Preparation method of biochar|[0041] Utilizing agricultural wastes such as facility tomato straws, wheat straws, peanut shells, rice hulls, garden trees and the like to crack for 3-4 hours at 300-500 ℃ under an anaerobic condition, crushing a cracking product to 1-2 mm by using a crusher, detecting nutrient content and physicochemical properties, and determining the detection method by referring to a soil sample analysis method, namely a quick-acting nitrogen alkali de-diffusion method; the quick-acting potassium and the total potassium are measured by flame photometry; measuring the quick-acting phosphorus by an Olsen-molybdenum-antimony colorimetric method; organic substance adopts TOC, measuring by using an analyzer; the total nitrogen is measured by adopting a semi-micro Kjeldahl method; all phosphorus warp H2SO4-HClO4After digestion, measuring by a molybdenum-antimony colorimetric method; the pH value is water: diluting the mixture according to the carbon ratio of 5:1, and measuring the mixture by a pH meter; and (4) determining the content of the water-soluble total salt by adopting a residue drying-mass method. The results are shown in Table 1.|[0042] TABLE 1 content of biochar nutrients and physicochemical properties from different agricultural waste sources|[0043] |[0044] |INVENTION MODE|[0045] Example 2|[0046] The tomato straw biochar prepared in the example 1 is added into a soilless culture substrate to improve the cucumber yield|[0047] 1. The experiment was designed in a randomized block, with 3 treatments, each repeated 3 times. Adding the tomato straw biochar into a commercial soilless culture substrate according to the mass ratio of 0% (B0), 3% (B3) and 5% (B5) (the volume ratio of the turf to the vermiculite to the perlite is 3:1:1), fully mixing, and filling into soilless culture pots (the length, the width and the height of each pot are 76cm, 42cm and 27cm, and each pot contains 10kg of culture substrate) for later use.|[0048] 2. Transplanting 3-4 true leaves of south China type cucumber variety 'Yulong', watering the matrix thoroughly 2 days before planting, planting 2 plants in each pot, processing 16 plants for planting, and watering for planting once after planting. And managing after planting according to a conventional soilless cucumber cultivation method. Watering the soilless culture nutrient solution fertilizer once every 2 days in the seedling stage (the EC value is 1.6), and watering the nutrient solution fertilizer once every day in the flowering and fruit setting stage; the temperature in the greenhouse is controlled to be 25 ℃ on average in the daytime and 20 ℃ on average at night; greenhouse humidity, illumination intensity and CO2The concentration is not controlled and is consistent with the natural condition.|[0049] 3. Harvesting: planting in 2019, 9 and 15 days, harvesting in 10 and 22 days, finishing harvesting in 11 and 09 days, harvesting commodity melons every day or every other day in the sitting melon period, and expressing the yield of each plant according to the cumulative yield of a cell.|[0050] Test results|[0051] 1. Influence of tomato straw biochar added into soilless culture substrate on cucumber growth|[0052] The plant height and stem thickness of the cucumber are measured in the cucumber sitting-cucumber full-season. As shown in fig. 1-a and fig. 1-B, the plant height and stem thickness of the cucumber were not significantly different from those of the control treatment (adding biochar 0) by adding 3% of biochar to the soilless culture substrate, while the plant height of the cucumber was significantly reduced by adding 5% of biochar to the soilless culture substrate without significantly affecting the stem thickness of the cucumber. Under each treatment condition, cucumber plant height and stem thickness measured at 3% charcoal treatment were the greatest.|[0053] 2. Influence of tomato straw biochar added into soilless culture substrate on cucumber yield|[0054] As shown in fig. 2-a and 2-B, the addition of 3% of tomato straw biochar to the soilless culture substrate significantly increased cucumber yield, which was 22.8% higher than the control treatment (0 added with biochar), while the addition of 5% of biochar decreased cucumber yield, which was 8.57% lower than the control treatment. This is probably due to the fact that the high salt content in the tomato seedling biochar and the organic compounds thereof, such as n-alkanoic acid, hydroxy and acetoxy acid-containing compounds, benzoic acid and phenols, are easily re-condensed into the biochar during the waste cracking and cooling process, and the compounds have a promoting effect (toxic excitation effect) on the growth of crops under the condition of low concentration and are harmful to the growth of crops under the condition of high concentration. Therefore, it is presumed that the high content of organic compounds and high salt contained in the vegetable soilless culture substrate to which the 3% tomato straw biochar is added inhibits the growth of cucumber. Therefore, the amount of the tomato straw biochar added into the soilless culture substrate is not higher than 5%, and the yield increase effect of the cucumber is the best by adding 3% biochar in the experimental example.|[0055] The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention. Family Number|(88264022)|88264022|Abstract|(CN110999751 A)|The invention provides a biochar prepared from facility agriculture wastes , a preparation method of the biochar , a soilless culture substrate and application of the soilless culture substrate , and belongs to the technical field of crop cultivation . The method for preparing the biochar from facility agriculture wastes comprises the following steps that the facility agriculture wastes are crushed and are then subjected to cracking for 3 to 4 h at 300 DEG C to 500 DEG C under the oxygen - free condition ; and obtained cracking products are crushed to obtain the biochar . The prepared biochar containsrich porous structures and nutritional ingredients including rapidly available potassium , rapidly available phosphorus , rapidly available nitrogen , organic matters and salts ; and the pH is alkaline , so that sufficient ventilation pores and nutrients are provided for crop growth . The invention also provides a vegetable soilless culture substrate containing the biochar . Compared with an existing soilless culture substrate , the vegetable soilless culture substrate provided by the invention has the advantages that the cucumber yield can be stably improved ; the cyclic utilization of facility agriculture production wastes such as straws can also be realized ; and carbon sequestration , emission reduction and green development are promoted . |CPC codes|(CN110999751 A)|A01G - 024/10 |A01G - 031/00 |C01B - 032/05 |IPC codes|(CN110999751 A)|A01G - 024/10 |A01G - 031/00 |C01B - 032/05 | Materials, metallurgy|Other special machines A01G-024/10|A01G-031/00|C01B-032/05|Y02P-060/21 A01G-024/10|A01G-031/00|C01B-032/05|Y02P-060/21 A01G-024/10|A01G-031/00|C01B-032/05 A01G-024/10|A01G-031/00|C01B-032/05 CN116250465|PL2022443188|CN114751394|CN113620744|CN116082092B|CN114946597B|CN114902930B CN116250465 105286799 WHO=Examiner SELF=Y CAT=Y CAT=X|PL2022443188 110563086 WHO=Examiner SELF=N CAT=A|CN114751394 100920433 WHO=Examiner SELF=N CAT=A|CN113620744 96887822 WHO=Examiner SELF=N CAT=A|CN116082092B 104871878 WHO=Examiner SELF=N|CN114946597B 101545147 WHO=Examiner SELF=N|CN114902930B 101335899 WHO=Examiner SELF=N LAPSED (CN110999751)|LAPSED DEAD (CN110999751)|DEAD (CN110999751)|LEGAL DETAILS FOR CN110999751|Actual or expected expiration date=2021-07-23|Legal state=DEAD|Status=LAPSED|Event publication date=2019-12-20|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201911324980|Application date=2019-12-20|Standardized application number=2019CN-1324980|Event publication date=2020-04-14|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN110999751|Publication stage code=A|Publication date=2020-04-14|Standardized publication number=CN110999751|Event publication date=2020-04-14|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2020-05-08|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2021-07-23|Event code=CN/WW01|Event indicator=Neg|Event group=Event indicating Not In Force|Withdrawal of patent application after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSSdg63hWWvllfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000035113642&ekey=2171&xpn=CN110999751&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=6djxPAnvF16GQUY%252FoKoDbZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN110999751)|CN (CN110999751)|NAME=QINGDAO ACADEMY OF AGRICULTURAL SCIENCES , COUNTRY=CN (CN110999751)|NAME=DONG DAYUAN;BEIJING GAOWO LAW FIRM , REG=11569 (CN110999751)|CN (CN110999751)|NAME=ZHANG GONGCHEN, COUNTRY=CN |NAME=WAN SHUWEI|NAME=ZHAO AIHONG|NAME=ZHANG SHOUCAI|NAME=LI LEI|NAME=QIN YUHONG|NAME=WANG BO|NAME=JIANG ZHIXUN|NAME=WANG ZHENQING|NAME=LIU LING|NAME=LI HAINING 0 1 Titre: (CN110999751)|Biochar prepared from facility agriculture wastes, preparation method of biochar, soilless culture substrate and application of soilless culture substrate Résumé: (CN110999751)|The invention provides a biochar prepared from facility agriculture wastes, a preparation method of the biochar, a soilless culture substrate and application of the soilless culture substrate, and belongs to the technical field of crop cultivation. The method for preparing the biochar from facility agriculture wastes comprises the following steps that the facility agriculture wastes are crushed and are then subjected to cracking for 3 to 4 h at 300 DEG C to 500 DEG C under the oxygen-free condition; and obtained cracking products are crushed to obtain the biochar. The prepared biochar containsrich porous structures and nutritional ingredients including rapidly available potassium, rapidly available phosphorus, rapidly available nitrogen, organic matters and salts; and the pH is alkaline,so that sufficient ventilation pores and nutrients are provided for crop growth. The invention also provides a vegetable soilless culture substrate containing the biochar. Compared with an existing soilless culture substrate, the vegetable soilless culture substrate provided by the invention has the advantages that the cucumber yield can be stably improved; the cyclic utilization of facility agriculture production wastes such as straws can also be realized; and carbon sequestration, emission reduction and green development are promoted. 89 Abstract gpt-4o-mini no The article focuses on biochar from agricultural wastes and its application in soilless culture, without a central emphasis on accelerated weathering or CO₂ capture.
91 CN202510094191 CN202510094191 CN119858921 114287066 CN119858921 A 2025-04-22 [CN119858921] 2025-01-21 2025-01-21 2025-04-22 (CN119858921)|2045-01-21 (CN119858921)|Regeneration and recovery method of silicon carbide in silicon melt refining slag (CN119858921)|The invention belongs to the technical field of secondary resource utilization, and relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag. The method realizes value-added recycling of the silicon melt refining slag. The method comprises the following steps: by taking silicon melt refining slag as a silicon source and a waste graphite component as a carbon source, crushing and grinding the silicon melt refining slag and the waste graphite component, adding waste graphite component powder into the silicon melt refining slag according to a weight ratio, uniformly mixing, putting into a high-temperature reaction furnace, and carrying out carbon thermal reduction smelting to prepare a sintered block containing silicon carbide; then crushing the sintered block containing silicon carbide and carrying out carbon removal treatment in air at different temperatures; and finally, carrying out acid pickling and drying on the carbon-removed silicon carbide powder to obtain the silicon carbide powder with high additional value. According to the method, the utilization rate of monatomic silicon in the silicon melt refining slag is high, the raw material applicability is high, resources are saved, the prepared silicon carbide is high in quality and uniform in particle size, high-value utilization of the silicon melt refining slag is achieved, and a new direction is provided for disposal of the silicon melt refining slag. KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY (CN119858921)|KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) CHEN ZHENGJIE|HU YIYOU|ZHANG YONGHANG|HU PANPAN|MA WENHUI|ZHANG YAKUN (CN119858921)|CHEN ZHENGJIE|HU YIYOU|ZHANG YONGHANG|HU PANPAN|MA WENHUI|ZHANG YAKUN (CN119858921)|JIANG TAIWEI;CHANGSHA RONG ZHI PATENT AGENCY|Reg. Nb: 43114 (CN119858921)|(4) Provides a new technical direction for the disposal of silicon melt refining slag, solves the problem that silicon carbide is difficult to remove, which is the difficult problem of purifying simple substance silicon from silicon melt refining slag, and realizes changing waste into valuables.| (CN119858921)|1. The regeneration and recovery method of silicon carbide in silicon melt refining slag is characterized by comprising the following steps: (1) Firstly, crushing and grinding silicon melt refining slag to obtain silicon slag powder with the particle size of-100 meshes, preferably 100-300 meshes, and crushing and grinding waste graphite to obtain waste graphite powder with the particle size of-100 meshes, preferably 100-300 meshes; (2) Mixing silicon melt refining slag powder and waste graphite powder according to a mass ratio of 0.5-2.5:1, preferably 1-2:1, and further preferably 1.5-1.9:1; (3) Placing the mixed material obtained in the step (2) into a crucible, and placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting to prepare a silicon carbide-containing sintered block, wherein the carbothermic reduction temperature is 1400-1600 ℃; (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and removing carbon through oxidization to obtain decarburized sintering powder; (5) And (3) carrying out acid washing and drying on the decarburized sintering powder obtained in the step (4) to obtain high-quality silicon carbide powder. | (CN119858921)|The invention provides the method for realizing high-value recycling of the silicon slag, reducing environmental pollution, improving the utilization rate of silicon resources, indirectly reducing the production cost of industrial silicon enterprises and realizing sustainable development.|The invention relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag, belonging to the technical field of secondary resource utilization.|The invention relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag, which comprises the following steps:| (CN119858921)|SILICON CARBIDE(100,183)|SLAG(100,58)|SILICON MELT(100,43)|REGENERATION(100,24)|SILICON CARBIDE RECOVERY(100,17)|DECARBURIZED SINTERING POWDER(100,4)|RESOURCE UTILIZATION(63,2)|GRINDING WASTE GRAPHITE(57,2)|SILICON MELT DISPOSAL(51,1)|WASTE GRAPHITE(50,6)|SILICON ENTERPRISE(48,1)|MOLTEN SLAG(43,9)|ACIDIC WASH(40,9)|CARBOTHERMIC REDUCTION SMELTING(39,13)|ISOSTATIC GRAPHITE(39,1)|SUBSTANCE SILICON(37,24)|CRUSHING(35,21)|RESOURCE SAVING(35,1)|SILICON MELT REFINING SLAG(35,1)|SINTERED BLOCK(34,26)|SILICON DISPOSAL(33,1)|CRUCIBLE(32,35)|SILICON POWDER REMELTING(31,2)|SILICON CARBIDE POWDER(30,27)|UNIFORM GRANULARITY(30,1)|RECYCLING SILICON CARBIDE(29,1)|SILICON SLAG(28,7)|SILICON POWDER REFINING(28,2)|REACTION FURNACE(27,13)|SILICON RESOURCE(27,3)|GRAPHITE COMPONENT POWDER RESIDUE(27,1)|SILICON MELT MIXING(26,12)|OXIDE(26,2)|REDUCING ENVIRONMENTAL POLLUTION(26,1)|WASTE GRAPHITE COMPONENT(23,16)|CARBOTHERMIC REDUCTION(23,3)|ENVIRONMENTAL POLLUTION(23,1)|WASTE GRAPHITE MEMBER(23,1)|CHANGING(22,2)|SUSTAINABLE DEVELOPMENT(22,1)|ACID WASHING PURIFICATION(19,20)|CARBOTHERMIC REDUCTION TEMPERATURE(17,2)|CARBON REMOVAL TREATMENT(16,1)|REMOVING CARBON(15,14)|GUIDE CYLINDER(15,11)|SUBSTANCE SILICON RECYCLING RATE(15,10)|GAS PROTECTION(15,2)|TECHNICAL DIRECTION(15,1)|ACIDIC WASH CONDITION(14,20)|CARBOTHERMIC REDUCTION REACTION(14,2)|MIXED ACID PICKLING TEMPERATURE(14,1)|HYDROFLUORIC ACID MIXED ACID(12,16)|PREPARED SILICON CARBIDE(12,4)|HYDROCHLORIC ACID PICKLING TEMPERATURE(12,2)|SUBSTANCE SILICON UTILIZATION RATE(11,5)|PARTICLE SIZE(11,4)|WEIGHT RATIO(11,1)|UTILIZATION RATE(10,6)|SILICON SOURCE(10,3)|ARGON(10,2)|SILICON VALUE ADDED RECYCLING(10,1)|ACIDIC WASH TEMPERATURE(9,20)|FIRE(9,3)|SHIELDING GAS(9,2)|SILICATE IMPURITY(9,2)|MIXED MATERIAL(7,12)|SILICON CARBIDE PHASE(7,10)|DIAMOND WIRE CUTTING SCRAP(7,2)|RAW MATERIAL APPLICABILITY(7,2)|RECYCLING SILICON SLAG(7,1)|SILICON RESOURCE AVOIDING WASTE(7,1)|WASTE GRAPHITE POWDER CONSUMPTION(7,1)|MASS RATIO(6,12)|ISOSTATIC PRESSURE GRAPHITE(6,2)|SILICIC ACID PRECIPITATION(6,2)|SMELTING MODE(6,2)|PURITY ELEMENTAL SILICON(6,1)|REFINING INDUSTRIAL SILICON(6,1)|SEPARATING SLAG SILICON(6,1)|NITRIC ACID VOLUME RATIO(5,13)|XRD PHASE(5,3)|HYDROCHLORIC ACID PICKLING TIME(5,2)|MIXED ACID PICKLING TIME(5,1)|SILICON CARBIDE AGGLOMERATE(5,1)|SILICON MELT UTILIZATION(5,1)|SILICON MELT XRD PATTERN(5,1)|ACIDIC WASH TIME(4,20)|AVERAGE PARTICLE SIZE(4,20)|SILICON CARBIDE PRODUCT(4,4)|SILICON DIOXIDE(4,4)|ANNUAL YIELD(4,1)|CRUCIBLE COMPONENT(4,1)|FLOATING SILICON(4,1)| (CN119858921)|1. The regeneration and recovery method of silicon carbide in silicon melt refining slag is characterized by comprising the following steps:| (1) Firstly, crushing and grinding silicon melt refining slag to obtain silicon slag powder with the particle size of-100 meshes, preferably 100-300 meshes, and crushing and grinding waste graphite to obtain waste graphite powder with the particle size of-100 meshes, preferably 100-300 meshes; | (2) Mixing silicon melt refining slag powder and waste graphite powder according to a mass ratio of 0.5-2.5:1, preferably 1-2:1, and further preferably 1.5-1.9:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, and placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting to prepare a silicon carbide-containing sintered block, wherein the carbothermic reduction temperature is 1400-1600 ℃; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and removing carbon through oxidization to obtain decarburized sintering powder; | (5) And (3) carrying out acid washing and drying on the decarburized sintering powder obtained in the step (4) to obtain high-quality silicon carbide powder. |2. The method for regenerating and recovering silicon carbide in silicon melt-refining slag according to claim 1, wherein the silicon melt-refining slag in the step (1) comprises, but is not limited to, molten slag after external refining of industrial silicon melt, molten slag after remelting of silicon powder and/or molten slag after fire refining of silicon powder;| the waste graphite members in step (1) include, but are not limited to, graphite members such as guide cylinders, thermal fields, crucibles, etc. made of isostatic graphite. |3. The method for regenerating and recovering silicon carbide in silicon melt refining slag according to claim 1, wherein the reaction temperature of carbothermic reduction reaction in the step (3) is 1450-1550 ℃, the reaction time is 1-4h, and protective gas is introduced in the reaction process.|4. The method for regenerating and recovering silicon carbide from a silicon melt refining slag according to claim 1, wherein the shielding gas is preferably argon.|5. The method for regenerating and recovering silicon carbide from a silicon melt refining slag according to claim 1, wherein the temperature for removing carbon in the step (4) is 600-800 ℃ and the time for removing carbon is 1-4 hours.|6. The method for regenerating and recovering silicon carbide from silicon melt refining slag according to claim 1, wherein the acid washing in the step (5) is performed by acid washing with hydrochloric acid once followed by acid washing with nitric acid and hydrofluoric acid mixed acid.|7. The method for regenerating and recovering silicon carbide in silicon melt refining slag according to claim 1, wherein the hydrochloric acid pickling temperature is 25-70 ℃, the hydrochloric acid pickling time is 1-4h, and the hydrochloric acid concentration is 0.5-3mol/L.|8. The method for regenerating and recovering silicon carbide in silicon melt refining slag according to claim 1, wherein the volume ratio of nitric acid to hydrofluoric acid in the mixed acid pickling process of nitric acid and hydrofluoric acid is 1-3:1, preferably 2-3:1, the mixed acid pickling temperature of nitric acid and hydrofluoric acid is 25-70 ℃, preferably 40-60 ℃, the mixed acid pickling time of nitric acid and hydrofluoric acid is 1-4h, the nitric acid concentration is 0.5-3mol/L, preferably 2-3mol/L, and the hydrofluoric acid concentration is 0.5-3mol/L.|9. The method for regenerating and recovering silicon carbide in silicon melt refining slag as defined in claim 1, wherein the method comprises the steps of:| The purity of the obtained silicon carbide is more than 95%, the recycling rate of the simple substance silicon in the silicon melt refining slag is more than 95%, the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is 0.5-1 mu m, D50 is 2-5 mu m, and D90 is 10-20 mu m. (CN119858921)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag, belonging to the technical field of secondary resource utilization.|BACKGROUND ART|[0002] Industrial silicon is an important basic chemical raw material and a strategic emerging material, is widely applied to the fields of chemical industry, electronics, solar energy, alloy, ceramics, glass, rubber and the like, has the annual yield of 375 ten thousand tons, and silicon melt refining slag (silicon slag for short) is solid waste generated in the process of blowing and refining industrial silicon, and mainly contains silicate (70-76 wt%), elemental silicon (15-20 wt%) and silicon carbide (4-8 wt%) and the like. The prior silicon melt refining slag is mainly used as solid waste for long-term storage, not only brings about environmental problems, but also causes waste of silicon resources, and related patents for recycling and utilizing the silicon melt refining slag at present comprise a method (CN 111232987B) for efficiently recycling simple substance silicon in industrial silicon slag, a light high-strength ceramsite based on the silicon slag and a preparation method (CN 116947529B) thereof, a method (CN 111232988B) for efficiently separating slag silicon in the industrial silicon slag, a method (CN 111822154B) for floating silicon from the silicon slag, a method (CN 113666376B) for recycling the silicon slag, and a method (CN 116574906A) for preparing silicon-calcium-aluminum alloy or silicon-calcium-aluminum-iron alloy from the industrial silicon slag. In the several inventions described above, the recovery and utilization of silicon melt refining slag mainly includes smelting to prepare high purity elemental silicon and silicon-containing alloys, and the use of such solid waste for preparing high quality silicon carbide is not currently involved in the prior art.|[0003] Silicon carbide has high hardness, high strength, high temperature resistance, corrosion resistance, various excellent performances, plays an important role in various fields, and has wide application prospect. The prior art has been concerned with the preparation of silicon carbide from a portion of the scrap, such as CN109734098a, which is concerned with the preparation of silicon carbide from diamond wire cutting scrap in combination with an organic carbonaceous reducing agent, but is not concerned with how to increase the recovery of silicon carbide, and CN107651690B, which is concerned with the preparation of silicon carbide from diamond wire cutting scrap, bonding, pelletizing the carbonaceous reducing agent, and then sintering the pellets coated with the carbonaceous reducing agent to obtain silicon carbide, is not concerned with how to increase the recovery of silicon carbide.|[0004] Meanwhile, the technology for preparing silicon carbide by carbon thermal reduction by taking silicon melt refining slag as a silicon source and waste graphite components as a carbon source through a mode of smelting before selecting is found to be fresh. The invention provides the method for realizing high-value recycling of the silicon slag, reducing environmental pollution, improving the utilization rate of silicon resources, indirectly reducing the production cost of industrial silicon enterprises and realizing sustainable development.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the current state of treatment of solid wastes such as silicon melt refining slag, the invention provides a regeneration and recovery method of silicon carbide in the silicon melt refining slag in a smelting-before-selecting mode, thereby realizing high-value treatment of the silicon melt refining slag, avoiding waste of silicon resources, changing waste into valuables, bringing industrial value-added, the purity of the silicon carbide prepared by the method is more than 95%, the recovery utilization rate of simple substance silicon in the silicon melt refining slag is more than 95%, and meanwhile, the obtained product has small particle size and narrow particle size distribution.|[0006] The invention relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag, which comprises the following steps:| (1) Firstly, crushing and grinding silicon melt refining slag to obtain silicon slag powder with the particle size of-100 meshes, preferably 100-300 meshes, and crushing and grinding waste graphite to obtain waste graphite powder with the particle size of-100 meshes, preferably 100-300 meshes; | (2) Mixing silicon melt refining slag powder and waste graphite powder according to a mass ratio of 0.5-2.5:1, preferably 1-2:1, and further preferably 1.5-1.9:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, and placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting to prepare a silicon carbide-containing sintered block, wherein the carbothermic reduction temperature is 1400-1600 ℃; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and removing carbon through oxidization to obtain decarburized sintering powder; | (5) And (3) carrying out acid washing and drying on the decarburized sintering powder obtained in the step (4) to obtain high-quality silicon carbide powder. |[0007] Preferably, the silicon melt refining slag in the step (1) comprises but is not limited to molten slag after external refining of industrial silicon melt, molten slag after remelting of silicon powder and/or molten slag after fire refining of silicon powder, and the waste graphite components in the step (1) comprise but are not limited to graphite components such as guide cylinders, thermal fields, crucibles and the like made of isostatic pressure graphite.|[0008] The proportion of the silicon melt refining slag powder and the waste graphite powder is controlled to be 1.5-1.9:1, and the silicon melt refining slag powder and the waste graphite powder are in the proportion, so that the silicon melt refining slag powder has better raw material applicability, simple substance silicon in the silicon melt refining slag can be fully reacted and converted into silicon carbide, the waste graphite powder can be fully utilized, if the consumption of the waste graphite powder is too small, the simple substance silicon in the silicon melt refining slag is not fully reacted, the purity of the prepared silicon carbide is not high, the purity of the prepared silicon carbide is higher than 95% in the proportion of 1.5-1.9, and the recycling rate of the simple substance silicon in the silicon melt refining slag is higher than 95%.|[0009] After the optimization, the granularity of the obtained silicon carbide product shows a certain normal distribution characteristic, wherein D10 is 0.5-1 mu m, D50 is 2-5 mu m, and D90 is 10-20 mu m.|[0010] Preferably, the reaction temperature of the carbothermic reaction in the step (3) is 1450-1550 ℃, the reaction time is 1-4h, and protective gas is introduced in the reaction process. The carbothermic reaction is controlled to 1450-1550 ℃ for 1-4h, so that the full reaction of the simple substance silicon in the silicon melt refining slag and the waste graphite is promoted, the purity of the prepared silicon carbide is ensured to be more than 95%, and the recycling rate of the simple substance silicon in the silicon melt refining slag is ensured to be more than 95%.|[0011] Preferably, the shielding gas is argon.|[0012] Preferably, the temperature for removing carbon in the step (4) is 600-800 ℃, and the time for removing carbon is 1-4 hours.|[0013] Preferably, the acid washing in the step (5) is carried out by first carrying out hydrochloric acid washing and then carrying out nitric acid and hydrofluoric acid mixed acid washing. Because the method adopts a mode of smelting before selecting, more than 50 percent of silicate impurities exist in the silicon melt refining slag, most of silicate impurities can be removed by one-time hydrochloric acid washing, a small amount of simple substance silicon and silicon dioxide in a silicon carbide product can be removed by mixed acid washing of nitric acid and hydrofluoric acid, the occurrence of silicic acid precipitation can be reduced by two-time acid washing, the impurity removal rate is improved, and the purity of the silicon carbide product is more than 95 percent.|[0014] Preferably, the hydrochloric acid pickling temperature is 25-70 ℃, the hydrochloric acid pickling time is 1-4h, and the hydrochloric acid concentration is 0.5-3mol/L.|[0015] Preferably, the volume ratio of nitric acid to hydrofluoric acid in the mixed acid pickling process of nitric acid and hydrofluoric acid is 1-3:1, preferably 2-3:1, the pickling temperature of the mixed acid of nitric acid and hydrofluoric acid is 25-70 ℃, preferably 40-60 ℃, the pickling time of the mixed acid of nitric acid and hydrofluoric acid is 1-4h, the concentration of nitric acid is 0.5-3mol/L, preferably 2-3mol/L, and the concentration of hydrofluoric acid is 0.5-3mol/L.|[0016] The beneficial effects of the invention are as follows:| (1) The invention prepares high-quality silicon carbide by taking low-added-value silicon melt refining slag as a raw material, and the added carbon source is a waste graphite component and also belongs to the category of solid waste, and the invention converts the low-cost silicon melt refining slag and the waste graphite component into silicon carbide with higher added value, wherein the purity of the silicon carbide is more than 95%; | (2) The silicon melt refining slag has high utilization rate of simple substance silicon, and the carbothermic reduction reaction between the silicon melt refining slag and the waste graphite component is sufficient, so that most of simple substance silicon in the silicon melt refining slag is converted into silicon carbide, and the utilization rate of the simple substance silicon is more than 95%; | (3) The invention adopts a preparation process of smelting before selecting, and the molten slag after refining the industrial silicon melt outside the furnace, the molten slag after remelting the silicon powder and/or the molten slag after fire refining the silicon powder, and waste graphite components such as guide cylinders, thermal fields, crucibles and the like made of isostatic pressure graphite can be used as the silicon source and the carbon source of the invention; | (4) Provides a new technical direction for the disposal of silicon melt refining slag, solves the problem that silicon carbide is difficult to remove, which is the difficult problem of purifying simple substance silicon from silicon melt refining slag, and realizes changing waste into valuables. |DRAWINGS DESCRIPTION|[0017] FIG. 1 is a process flow diagram of the present invention.|[0018] FIG. 2 is an XRD pattern of silicon melt refining slag, high temperature carbothermic reduction smelting of silicon carbide agglomerates, crushing of carbon-removed silicon carbide powder, and pickling, drying and purification of silicon carbide powder in example 1.|[0019] FIG. 3 is a graph showing the particle size distribution in the laser particle size measurement report of the silicon carbide product of example 1.|INVENTION MODE|Detailed Description|[0020] The invention will be described in further detail with reference to the following specific embodiments, but the scope of the invention is not limited to the description.|[0021] Example 1|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a guide cylinder, are crushed and ground into graphite powder with the average particle size of 200 meshes. The main components of the silicon melt refining slag are silicate (69.50 wt%), elemental silicon (21.60 wt%), silicon carbide (8.90 wt%), and the main components of the guide cylinder are graphite (73.60 wt%), silicon carbide (14.30 wt%), elemental silicon (10.10 wt%) and the balance of impurities. |[0022] (2) Mixing silicon melt refining slag powder and guide cylinder powder according to the mass ratio of 1.5:1;| (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 750 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2h, the hydrochloric acid concentration is 1 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 2h, the nitric acid concentration is 3mol/L and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0023] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection.|[0024] The purity of the obtained silicon carbide is 96.34%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 96.30%, the granularity of the silicon carbide shows a certain normal distribution characteristic, wherein D10 is about 0.7-0.8 mu m, D50 is about 2.9-3.1 mu m, D90 is about 15-16 mu m, and specific numerical values are shown in figure 3.|[0025] Example 2|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) The silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 150 meshes, and the waste graphite component, namely the guide cylinder, is crushed and ground into graphite powder with the average particle size of 150 meshes. The main components of the silicon melt refining slag are silicate (69.70 wt%), elemental silicon (21.90 wt%), silicon carbide (8.40 wt%), and the main components of the guide cylinder are graphite (74.20 wt%), silicon carbide (12.60 wt%), and elemental silicon (13.20 wt%); | (2) Mixing silicon melt refining slag powder and guide cylinder powder according to the mass ratio of 1.5:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1550 ℃ to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 750 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 1h, the hydrochloric acid concentration is 2 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 2:1, the acid washing temperature of the nitric acid and hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and hydrofluoric acid mixed acid is 3h, the nitric acid concentration is 2mol/L, and the hydrofluoric acid concentration is 2 mol/L), and drying to obtain the silicon carbide powder. |[0026] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 96.20%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 95.85%, and the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.7-0.8 mu m, D50 is about 3.0-3.2 mu m, and D90 is about 15-16 mu m.|[0027] Example 3|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a thermal field, are crushed and ground into graphite powder with the average particle size of 200 meshes. Wherein the main components of the silicon melt refining slag are silicate (70.20 wt%), elemental silicon (22.70 wt%), silicon carbide (7.10 wt%), and the main components of the thermal field are graphite (97.70 wt%), and silicon carbide (2.30 wt%); | (2) Mixing silicon melt refining slag powder and thermal field powder according to a mass ratio of 1.6:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 3h, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 700 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 3 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 25 ℃, the acid washing time is 4 hours, the hydrochloric acid concentration is 3 mol/L), continuously carrying out acid washing purification by adopting nitric acid and hydrofluoric acid mixed acid (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and hydrofluoric acid mixed acid is 25 ℃, the acid washing time of the nitric acid and hydrofluoric acid mixed acid is 4 hours, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0028] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 95.60%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 96.20%, the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.74-0.76 mu m, D50 is about 3.1-3.15 mu m, and D90 is about 15.3-15.6 mu m.|[0029] Example 4|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) The silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 250 meshes, and the waste graphite component-thermal field is crushed and ground into graphite powder with the average particle size of 250 meshes. Wherein the main components of the silicon melt refining slag are silicate (71.45 wt%), elemental silicon (19.40 wt%), silicon carbide (9.15 wt%), and the main components of the thermal field are graphite (98.30 wt%), and silicon carbide (1.70 wt%); | (2) Mixing silicon melt refining slag powder and thermal field powder according to a mass ratio of 1.5:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 4 hours, and the reaction temperature is 1450 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 800 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 1.5h; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 70 ℃, the acid washing time is 1h, the hydrochloric acid concentration is 3 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and hydrofluoric acid mixed acid is 70 ℃, the acid washing time of the nitric acid and hydrofluoric acid mixed acid is 1h, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0030] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 95.30%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 95.00%, and the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.74-0.76 mu m, D50 is about 3.0-3.15 mu m, and D90 is about 15.4-15.7 mu m.|[0031] Example 5|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Crushing and grinding silicon melt refining slag into silicon slag powder with the average particle size of 300 meshes, and crushing and grinding waste graphite components, namely a crucible, into graphite powder with the average particle size of 300 meshes, wherein the silicon melt refining slag comprises main components of silicate (72.30 wt%), elemental silicon (20.30 wt%), silicon carbide (7.40 wt%), and the crucible comprises main components of graphite (95.30 wt%), silicon dioxide (2.80 wt%), metal oxides (1.90 wt% of ferric oxide, calcium oxide and the like); | (2) Mixing silicon melt refining slag powder and crucible powder according to a mass ratio of 1.7:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 650 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 4 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2 hours, the hydrochloric acid concentration is 3 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 1:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 3.5 hours, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0032] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 95.10%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 96.70%, and the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.74-0.76 mu m, D50 is about 3.0-3.05 mu m, and D90 is about 15.5-15.8 mu m.|[0033] Example 6|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a crucible, are crushed and ground into graphite powder with the average particle size of 180 meshes. The main components of the silicon melt refining slag are silicate (70.50 wt%), elemental silicon (21.40 wt%), silicon carbide (8.10 wt%), and the main components of the crucible are graphite (96.70 wt%), silicon dioxide (2.40 wt%), and metal oxides (0.90 wt% of ferric oxide, calcium oxide and the like); | (2) Mixing silicon melt refining slag powder and crucible powder according to a mass ratio of 1.9:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1550 ℃ to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 750 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 70 ℃, the acid washing time is 4h, the hydrochloric acid concentration is 0.5 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 70 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 4h, the nitric acid concentration is 0.5mol/L, and the hydrofluoric acid concentration is 0.5 mol/L), and drying to obtain the silicon carbide powder. |[0034] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 96.10%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 96.30%, and the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.76-0.8 mu m, D50 is about 3.05-3.15 mu m, and D90 is about 15.5-15.7 mu m.|[0035] Comparative example 1|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a guide cylinder, are crushed and ground into graphite powder with the average particle size of 200 meshes. The main components of the silicon melt refining slag are silicate (69.50 wt%), elemental silicon (21.60 wt%), silicon carbide (8.90 wt%), and the main components of the guide cylinder are graphite (73.60 wt%), silicon carbide (14.30 wt%), elemental silicon (10.10 wt%) and the balance of impurities. |[0036] (2) Mixing silicon melt refining slag powder and guide cylinder powder according to a mass ratio of 3:1;| (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 750 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2 hours, the hydrochloric acid concentration is 3 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 1:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 1 hour, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0037] The silicon carbide powder prepared in this comparative example was examined by XRD phase to have impurity phase silicon phase in addition to silicon carbide phase.|[0038] The purity of the obtained silicon carbide is 82.00%, the recovery and utilization rate of the simple substance silicon in the silicon melt refining slag is 79.30%, the granularity D10 of the silicon carbide is 102.75 mu m, the D50 of the silicon carbide is 303.41 mu m, and the D90 of the silicon carbide is 708.45 mu m.|[0039] Comparative example 2|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) The silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 50 meshes, and the waste graphite component, namely the guide cylinder, is crushed and ground into graphite powder with the average particle size of 50 meshes. The main components of the silicon melt refining slag are silicate (71.50 wt%), elemental silicon (21.60 wt%), silicon carbide (6.90 wt%), and the main components of the guide cylinder are graphite (74.20 wt%), silicon carbide (13.30 wt%) and elemental silicon (12.50 wt%). |[0040] (2) Mixing silicon melt refining slag powder and guide cylinder powder according to a mass ratio of 1:1;| (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 550 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2h, the hydrochloric acid concentration is 3 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 2h, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0041] The silicon carbide powder prepared in this comparative example was examined by XRD phase to have impurity phase carbon phase in addition to silicon carbide phase.|[0042] The purity of the obtained silicon carbide is 87.30%, the recovery and utilization rate of the simple substance silicon in the silicon melt refining slag is 88.50%, the granularity D10 of the silicon carbide is 95.63 mu m, the D50 is 274.33 mu m, and the D90 is 598.31 mu m.|[0043] Comparative example 3|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Crushing and grinding silicon melt refining slag into silicon slag powder with the average particle size of 180 meshes, and crushing and grinding waste graphite components, namely a crucible, into graphite powder with the average particle size of 180 meshes, wherein the silicon melt refining slag comprises main components of silicate (72.30 wt%), elemental silicon (20.30 wt%), silicon carbide (7.40 wt%), and the crucible comprises main components of graphite (95.30 wt%), silicon dioxide (2.80 wt%), metal oxides (1.90 wt% of ferric oxide, calcium oxide and the like); | (2) Mixing silicon melt refining slag powder and crucible powder according to a mass ratio of 1.5:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1350 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 700 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2 hours, the hydrochloric acid concentration is 3 mol/L), continuously carrying out acid washing purification by adopting nitric acid and hydrofluoric acid mixed acid after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 0.5:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 25 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 1 hour, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0044] The silicon carbide powder prepared in this comparative example was found to have an impurity phase silicon phase and carbon phase in addition to the silicon carbide phase by XRD phase detection.|[0045] The purity of the obtained silicon carbide is 53.40%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 48.60%, the granularity D10 of the silicon carbide is 143.53 mu m, the D50 of the silicon carbide is 397.33 mu m, and the D90 of the silicon carbide is 867.37 mu m.|[0046] The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a thermal field, are crushed and ground into graphite powder with the average particle size of 200 meshes. Wherein the main components of the silicon melt refining slag are silicate (70.20 wt%), elemental silicon (22.70 wt%), silicon carbide (7.10 wt%), and the main components of the thermal field are graphite (97.70 wt%), and silicon carbide (2.30 wt%); | (2) Mixing silicon melt refining slag powder and thermal field powder according to the mass ratio of 0.5:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 1h, and the reaction temperature is 1400 ℃ to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 500 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 3 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 25 ℃, the acid washing time is 1h, the hydrochloric acid concentration is 1 mol/L), continuously carrying out acid washing purification by adopting nitric acid and hydrofluoric acid mixed acid after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 25 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 1h, the nitric acid concentration is 1mol/L, and the hydrofluoric acid concentration is 1 mol/L), and drying to obtain the silicon carbide powder. |[0047] The silicon carbide powder prepared in this comparative example has been examined by XRD phase to show that impurity phases such as silicon phase, carbon phase and silicate phase are present in addition to the silicon carbide phase.|[0048] The silicon carbide prepared in this comparative example has excess carbon which is not removed, the purity of the obtained silicon carbide is 72.60%, the recovery rate of the simple substance silicon in the silicon melt refining slag is 68.60%, the granularity D10 of the silicon carbide is 118.67 mu m, the D50 is 353.41 mu m, and the D90 is 788.43 mu m.|[0049] Comparative example 5|Other conditions were identical to example 1 except that:| (5) And (3) directly carrying out pickling purification on the silicon carbide-containing powder obtained in the step (4) by adopting nitric acid and hydrofluoric acid mixed acid (wherein the pickling condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the pickling temperature of the nitric acid and hydrofluoric acid mixed acid is 50 ℃, the pickling time of the nitric acid and hydrofluoric acid mixed acid is 2h, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0050] The silicon carbide prepared by the comparative example has more silicic acid precipitation during filtration after acid washing and purification of nitric acid and hydrofluoric acid mixed acid, the purity of the obtained silicon carbide is 68.30%, the silicon recycling rate in silicon melt refining slag is 71.50%, the granularity D10 of the silicon carbide is 178.27 mu m, the granularity D50 of the silicon carbide is 393.44 mu m, and the granularity D90 of the silicon carbide is 903.69 mu m.|[0051] While the present invention has been described in detail with reference to the specific embodiments thereof, the present invention is not limited to the above embodiments, and various changes can be made within the knowledge of those skilled in the art without departing from the spirit of the present invention. (CN119858921)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag, belonging to the technical field of secondary resource utilization.|BACKGROUND ART|[0002] Industrial silicon is an important basic chemical raw material and a strategic emerging material, is widely applied to the fields of chemical industry, electronics, solar energy, alloy, ceramics, glass, rubber and the like, has the annual yield of 375 ten thousand tons, and silicon melt refining slag (silicon slag for short) is solid waste generated in the process of blowing and refining industrial silicon, and mainly contains silicate (70-76 wt%), elemental silicon (15-20 wt%) and silicon carbide (4-8 wt%) and the like. The prior silicon melt refining slag is mainly used as solid waste for long-term storage, not only brings about environmental problems, but also causes waste of silicon resources, and related patents for recycling and utilizing the silicon melt refining slag at present comprise a method (CN 111232987B) for efficiently recycling simple substance silicon in industrial silicon slag, a light high-strength ceramsite based on the silicon slag and a preparation method (CN 116947529B) thereof, a method (CN 111232988B) for efficiently separating slag silicon in the industrial silicon slag, a method (CN 111822154B) for floating silicon from the silicon slag, a method (CN 113666376B) for recycling the silicon slag, and a method (CN 116574906A) for preparing silicon-calcium-aluminum alloy or silicon-calcium-aluminum-iron alloy from the industrial silicon slag. In the several inventions described above, the recovery and utilization of silicon melt refining slag mainly includes smelting to prepare high purity elemental silicon and silicon-containing alloys, and the use of such solid waste for preparing high quality silicon carbide is not currently involved in the prior art.|[0003] Silicon carbide has high hardness, high strength, high temperature resistance, corrosion resistance, various excellent performances, plays an important role in various fields, and has wide application prospect. The prior art has been concerned with the preparation of silicon carbide from a portion of the scrap, such as CN109734098a, which is concerned with the preparation of silicon carbide from diamond wire cutting scrap in combination with an organic carbonaceous reducing agent, but is not concerned with how to increase the recovery of silicon carbide, and CN107651690B, which is concerned with the preparation of silicon carbide from diamond wire cutting scrap, bonding, pelletizing the carbonaceous reducing agent, and then sintering the pellets coated with the carbonaceous reducing agent to obtain silicon carbide, is not concerned with how to increase the recovery of silicon carbide.|[0004] Meanwhile, the technology for preparing silicon carbide by carbon thermal reduction by taking silicon melt refining slag as a silicon source and waste graphite components as a carbon source through a mode of smelting before selecting is found to be fresh. The invention provides the method for realizing high-value recycling of the silicon slag, reducing environmental pollution, improving the utilization rate of silicon resources, indirectly reducing the production cost of industrial silicon enterprises and realizing sustainable development.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the current state of treatment of solid wastes such as silicon melt refining slag, the invention provides a regeneration and recovery method of silicon carbide in the silicon melt refining slag in a smelting-before-selecting mode, thereby realizing high-value treatment of the silicon melt refining slag, avoiding waste of silicon resources, changing waste into valuables, bringing industrial value-added, the purity of the silicon carbide prepared by the method is more than 95%, the recovery utilization rate of simple substance silicon in the silicon melt refining slag is more than 95%, and meanwhile, the obtained product has small particle size and narrow particle size distribution.|[0006] The invention relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag, which comprises the following steps:| (1) Firstly, crushing and grinding silicon melt refining slag to obtain silicon slag powder with the particle size of-100 meshes, preferably 100-300 meshes, and crushing and grinding waste graphite to obtain waste graphite powder with the particle size of-100 meshes, preferably 100-300 meshes; | (2) Mixing silicon melt refining slag powder and waste graphite powder according to a mass ratio of 0.5-2.5:1, preferably 1-2:1, and further preferably 1.5-1.9:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, and placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting to prepare a silicon carbide-containing sintered block, wherein the carbothermic reduction temperature is 1400-1600 ℃; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and removing carbon through oxidization to obtain decarburized sintering powder; | (5) And (3) carrying out acid washing and drying on the decarburized sintering powder obtained in the step (4) to obtain high-quality silicon carbide powder. |[0007] Preferably, the silicon melt refining slag in the step (1) comprises but is not limited to molten slag after external refining of industrial silicon melt, molten slag after remelting of silicon powder and/or molten slag after fire refining of silicon powder, and the waste graphite components in the step (1) comprise but are not limited to graphite components such as guide cylinders, thermal fields, crucibles and the like made of isostatic pressure graphite.|[0008] The proportion of the silicon melt refining slag powder and the waste graphite powder is controlled to be 1.5-1.9:1, and the silicon melt refining slag powder and the waste graphite powder are in the proportion, so that the silicon melt refining slag powder has better raw material applicability, simple substance silicon in the silicon melt refining slag can be fully reacted and converted into silicon carbide, the waste graphite powder can be fully utilized, if the consumption of the waste graphite powder is too small, the simple substance silicon in the silicon melt refining slag is not fully reacted, the purity of the prepared silicon carbide is not high, the purity of the prepared silicon carbide is higher than 95% in the proportion of 1.5-1.9, and the recycling rate of the simple substance silicon in the silicon melt refining slag is higher than 95%.|[0009] After the optimization, the granularity of the obtained silicon carbide product shows a certain normal distribution characteristic, wherein D10 is 0.5-1 mu m, D50 is 2-5 mu m, and D90 is 10-20 mu m.|[0010] Preferably, the reaction temperature of the carbothermic reaction in the step (3) is 1450-1550 ℃, the reaction time is 1-4h, and protective gas is introduced in the reaction process. The carbothermic reaction is controlled to 1450-1550 ℃ for 1-4h, so that the full reaction of the simple substance silicon in the silicon melt refining slag and the waste graphite is promoted, the purity of the prepared silicon carbide is ensured to be more than 95%, and the recycling rate of the simple substance silicon in the silicon melt refining slag is ensured to be more than 95%.|[0011] Preferably, the shielding gas is argon.|[0012] Preferably, the temperature for removing carbon in the step (4) is 600-800 ℃, and the time for removing carbon is 1-4 hours.|[0013] Preferably, the acid washing in the step (5) is carried out by first carrying out hydrochloric acid washing and then carrying out nitric acid and hydrofluoric acid mixed acid washing. Because the method adopts a mode of smelting before selecting, more than 50 percent of silicate impurities exist in the silicon melt refining slag, most of silicate impurities can be removed by one-time hydrochloric acid washing, a small amount of simple substance silicon and silicon dioxide in a silicon carbide product can be removed by mixed acid washing of nitric acid and hydrofluoric acid, the occurrence of silicic acid precipitation can be reduced by two-time acid washing, the impurity removal rate is improved, and the purity of the silicon carbide product is more than 95 percent.|[0014] Preferably, the hydrochloric acid pickling temperature is 25-70 ℃, the hydrochloric acid pickling time is 1-4h, and the hydrochloric acid concentration is 0.5-3mol/L.|[0015] Preferably, the volume ratio of nitric acid to hydrofluoric acid in the mixed acid pickling process of nitric acid and hydrofluoric acid is 1-3:1, preferably 2-3:1, the pickling temperature of the mixed acid of nitric acid and hydrofluoric acid is 25-70 ℃, preferably 40-60 ℃, the pickling time of the mixed acid of nitric acid and hydrofluoric acid is 1-4h, the concentration of nitric acid is 0.5-3mol/L, preferably 2-3mol/L, and the concentration of hydrofluoric acid is 0.5-3mol/L.|[0016] The beneficial effects of the invention are as follows:| (1) The invention prepares high-quality silicon carbide by taking low-added-value silicon melt refining slag as a raw material, and the added carbon source is a waste graphite component and also belongs to the category of solid waste, and the invention converts the low-cost silicon melt refining slag and the waste graphite component into silicon carbide with higher added value, wherein the purity of the silicon carbide is more than 95%; | (2) The silicon melt refining slag has high utilization rate of simple substance silicon, and the carbothermic reduction reaction between the silicon melt refining slag and the waste graphite component is sufficient, so that most of simple substance silicon in the silicon melt refining slag is converted into silicon carbide, and the utilization rate of the simple substance silicon is more than 95%; | (3) The invention adopts a preparation process of smelting before selecting, and the molten slag after refining the industrial silicon melt outside the furnace, the molten slag after remelting the silicon powder and/or the molten slag after fire refining the silicon powder, and waste graphite components such as guide cylinders, thermal fields, crucibles and the like made of isostatic pressure graphite can be used as the silicon source and the carbon source of the invention; | (4) Provides a new technical direction for the disposal of silicon melt refining slag, solves the problem that silicon carbide is difficult to remove, which is the difficult problem of purifying simple substance silicon from silicon melt refining slag, and realizes changing waste into valuables. |DRAWINGS DESCRIPTION|[0017] FIG. 1 is a process flow diagram of the present invention.|[0018] FIG. 2 is an XRD pattern of silicon melt refining slag, high temperature carbothermic reduction smelting of silicon carbide agglomerates, crushing of carbon-removed silicon carbide powder, and pickling, drying and purification of silicon carbide powder in example 1.|[0019] FIG. 3 is a graph showing the particle size distribution in the laser particle size measurement report of the silicon carbide product of example 1.|INVENTION MODE|Detailed Description|[0020] The invention will be described in further detail with reference to the following specific embodiments, but the scope of the invention is not limited to the description.|[0021] Example 1|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a guide cylinder, are crushed and ground into graphite powder with the average particle size of 200 meshes. The main components of the silicon melt refining slag are silicate (69.50 wt%), elemental silicon (21.60 wt%), silicon carbide (8.90 wt%), and the main components of the guide cylinder are graphite (73.60 wt%), silicon carbide (14.30 wt%), elemental silicon (10.10 wt%) and the balance of impurities. |[0022] (2) Mixing silicon melt refining slag powder and guide cylinder powder according to the mass ratio of 1.5:1;| (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 750 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2h, the hydrochloric acid concentration is 1 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 2h, the nitric acid concentration is 3mol/L and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0023] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection.|[0024] The purity of the obtained silicon carbide is 96.34%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 96.30%, the granularity of the silicon carbide shows a certain normal distribution characteristic, wherein D10 is about 0.7-0.8 mu m, D50 is about 2.9-3.1 mu m, D90 is about 15-16 mu m, and specific numerical values are shown in figure 3.|[0025] Example 2|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) The silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 150 meshes, and the waste graphite component, namely the guide cylinder, is crushed and ground into graphite powder with the average particle size of 150 meshes. The main components of the silicon melt refining slag are silicate (69.70 wt%), elemental silicon (21.90 wt%), silicon carbide (8.40 wt%), and the main components of the guide cylinder are graphite (74.20 wt%), silicon carbide (12.60 wt%), and elemental silicon (13.20 wt%); | (2) Mixing silicon melt refining slag powder and guide cylinder powder according to the mass ratio of 1.5:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1550 ℃ to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 750 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 1h, the hydrochloric acid concentration is 2 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 2:1, the acid washing temperature of the nitric acid and hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and hydrofluoric acid mixed acid is 3h, the nitric acid concentration is 2mol/L, and the hydrofluoric acid concentration is 2 mol/L), and drying to obtain the silicon carbide powder. |[0026] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 96.20%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 95.85%, and the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.7-0.8 mu m, D50 is about 3.0-3.2 mu m, and D90 is about 15-16 mu m.|[0027] Example 3|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a thermal field, are crushed and ground into graphite powder with the average particle size of 200 meshes. Wherein the main components of the silicon melt refining slag are silicate (70.20 wt%), elemental silicon (22.70 wt%), silicon carbide (7.10 wt%), and the main components of the thermal field are graphite (97.70 wt%), and silicon carbide (2.30 wt%); | (2) Mixing silicon melt refining slag powder and thermal field powder according to a mass ratio of 1.6:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 3h, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 700 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 3 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 25 ℃, the acid washing time is 4 hours, the hydrochloric acid concentration is 3 mol/L), continuously carrying out acid washing purification by adopting nitric acid and hydrofluoric acid mixed acid (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and hydrofluoric acid mixed acid is 25 ℃, the acid washing time of the nitric acid and hydrofluoric acid mixed acid is 4 hours, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0028] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 95.60%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 96.20%, the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.74-0.76 mu m, D50 is about 3.1-3.15 mu m, and D90 is about 15.3-15.6 mu m.|[0029] Example 4|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) The silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 250 meshes, and the waste graphite component-thermal field is crushed and ground into graphite powder with the average particle size of 250 meshes. Wherein the main components of the silicon melt refining slag are silicate (71.45 wt%), elemental silicon (19.40 wt%), silicon carbide (9.15 wt%), and the main components of the thermal field are graphite (98.30 wt%), and silicon carbide (1.70 wt%); | (2) Mixing silicon melt refining slag powder and thermal field powder according to a mass ratio of 1.5:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 4 hours, and the reaction temperature is 1450 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 800 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 1.5h; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 70 ℃, the acid washing time is 1h, the hydrochloric acid concentration is 3 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and hydrofluoric acid mixed acid is 70 ℃, the acid washing time of the nitric acid and hydrofluoric acid mixed acid is 1h, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0030] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 95.30%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 95.00%, and the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.74-0.76 mu m, D50 is about 3.0-3.15 mu m, and D90 is about 15.4-15.7 mu m.|[0031] Example 5|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Crushing and grinding silicon melt refining slag into silicon slag powder with the average particle size of 300 meshes, and crushing and grinding waste graphite components, namely a crucible, into graphite powder with the average particle size of 300 meshes, wherein the silicon melt refining slag comprises main components of silicate (72.30 wt%), elemental silicon (20.30 wt%), silicon carbide (7.40 wt%), and the crucible comprises main components of graphite (95.30 wt%), silicon dioxide (2.80 wt%), metal oxides (1.90 wt% of ferric oxide, calcium oxide and the like); | (2) Mixing silicon melt refining slag powder and crucible powder according to a mass ratio of 1.7:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 650 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 4 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2 hours, the hydrochloric acid concentration is 3 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 1:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 3.5 hours, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0032] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 95.10%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 96.70%, and the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.74-0.76 mu m, D50 is about 3.0-3.05 mu m, and D90 is about 15.5-15.8 mu m.|[0033] Example 6|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a crucible, are crushed and ground into graphite powder with the average particle size of 180 meshes. The main components of the silicon melt refining slag are silicate (70.50 wt%), elemental silicon (21.40 wt%), silicon carbide (8.10 wt%), and the main components of the crucible are graphite (96.70 wt%), silicon dioxide (2.40 wt%), and metal oxides (0.90 wt% of ferric oxide, calcium oxide and the like); | (2) Mixing silicon melt refining slag powder and crucible powder according to a mass ratio of 1.9:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1550 ℃ to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 750 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 70 ℃, the acid washing time is 4h, the hydrochloric acid concentration is 0.5 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 70 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 4h, the nitric acid concentration is 0.5mol/L, and the hydrofluoric acid concentration is 0.5 mol/L), and drying to obtain the silicon carbide powder. |[0034] The silicon carbide powder prepared in the embodiment has only a single silicon carbide phase and no other impurity phases through XRD phase detection. The purity of the obtained silicon carbide is 96.10%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 96.30%, and the granularity of the silicon carbide presents a certain normal distribution characteristic, wherein D10 is about 0.76-0.8 mu m, D50 is about 3.05-3.15 mu m, and D90 is about 15.5-15.7 mu m.|[0035] Comparative example 1|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a guide cylinder, are crushed and ground into graphite powder with the average particle size of 200 meshes. The main components of the silicon melt refining slag are silicate (69.50 wt%), elemental silicon (21.60 wt%), silicon carbide (8.90 wt%), and the main components of the guide cylinder are graphite (73.60 wt%), silicon carbide (14.30 wt%), elemental silicon (10.10 wt%) and the balance of impurities. |[0036] (2) Mixing silicon melt refining slag powder and guide cylinder powder according to a mass ratio of 3:1;| (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 750 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2 hours, the hydrochloric acid concentration is 3 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 1:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 1 hour, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0037] The silicon carbide powder prepared in this comparative example was examined by XRD phase to have impurity phase silicon phase in addition to silicon carbide phase.|[0038] The purity of the obtained silicon carbide is 82.00%, the recovery and utilization rate of the simple substance silicon in the silicon melt refining slag is 79.30%, the granularity D10 of the silicon carbide is 102.75 mu m, the D50 of the silicon carbide is 303.41 mu m, and the D90 of the silicon carbide is 708.45 mu m.|[0039] Comparative example 2|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) The silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 50 meshes, and the waste graphite component, namely the guide cylinder, is crushed and ground into graphite powder with the average particle size of 50 meshes. The main components of the silicon melt refining slag are silicate (71.50 wt%), elemental silicon (21.60 wt%), silicon carbide (6.90 wt%), and the main components of the guide cylinder are graphite (74.20 wt%), silicon carbide (13.30 wt%) and elemental silicon (12.50 wt%). |[0040] (2) Mixing silicon melt refining slag powder and guide cylinder powder according to a mass ratio of 1:1;| (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1500 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 550 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2h, the hydrochloric acid concentration is 3 mol/L), continuously adopting nitric acid and hydrofluoric acid mixed acid to carry out acid washing purification after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 50 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 2h, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0041] The silicon carbide powder prepared in this comparative example was examined by XRD phase to have impurity phase carbon phase in addition to silicon carbide phase.|[0042] The purity of the obtained silicon carbide is 87.30%, the recovery and utilization rate of the simple substance silicon in the silicon melt refining slag is 88.50%, the granularity D10 of the silicon carbide is 95.63 mu m, the D50 is 274.33 mu m, and the D90 is 598.31 mu m.|[0043] Comparative example 3|The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Crushing and grinding silicon melt refining slag into silicon slag powder with the average particle size of 180 meshes, and crushing and grinding waste graphite components, namely a crucible, into graphite powder with the average particle size of 180 meshes, wherein the silicon melt refining slag comprises main components of silicate (72.30 wt%), elemental silicon (20.30 wt%), silicon carbide (7.40 wt%), and the crucible comprises main components of graphite (95.30 wt%), silicon dioxide (2.80 wt%), metal oxides (1.90 wt% of ferric oxide, calcium oxide and the like); | (2) Mixing silicon melt refining slag powder and crucible powder according to a mass ratio of 1.5:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 2 hours, and the reaction temperature is 1350 ℃, so as to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 700 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 2 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 50 ℃, the acid washing time is 2 hours, the hydrochloric acid concentration is 3 mol/L), continuously carrying out acid washing purification by adopting nitric acid and hydrofluoric acid mixed acid after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 0.5:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 25 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 1 hour, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0044] The silicon carbide powder prepared in this comparative example was found to have an impurity phase silicon phase and carbon phase in addition to the silicon carbide phase by XRD phase detection.|[0045] The purity of the obtained silicon carbide is 53.40%, the recycling rate of the simple substance silicon in the silicon melt refining slag is 48.60%, the granularity D10 of the silicon carbide is 143.53 mu m, the D50 of the silicon carbide is 397.33 mu m, and the D90 of the silicon carbide is 867.37 mu m.|[0046] The regeneration and recovery method of silicon carbide in silicon melt refining slag comprises the following steps:| (1) Silicon melt refining slag is crushed and ground into silicon slag powder with the average particle size of 200 meshes, and waste graphite components, namely a thermal field, are crushed and ground into graphite powder with the average particle size of 200 meshes. Wherein the main components of the silicon melt refining slag are silicate (70.20 wt%), elemental silicon (22.70 wt%), silicon carbide (7.10 wt%), and the main components of the thermal field are graphite (97.70 wt%), and silicon carbide (2.30 wt%); | (2) Mixing silicon melt refining slag powder and thermal field powder according to the mass ratio of 0.5:1; | (3) Placing the mixed material obtained in the step (2) into a crucible, placing the crucible into a high-temperature reaction furnace for carbothermic reduction smelting, wherein the reaction time is 1h, and the reaction temperature is 1400 ℃ to prepare a sintered block containing silicon carbide; | (4) Crushing and grinding the sintered blocks containing silicon carbide prepared in the step (3), and then removing carbon at 500 ℃ to obtain silicon carbide-containing powder, wherein the carbon removal time is 3 hours; | (5) And (3) carrying out acid washing purification on the silicon carbide-containing powder obtained in the step (4) by adopting hydrochloric acid (wherein the acid washing condition is that the acid washing temperature is 25 ℃, the acid washing time is 1h, the hydrochloric acid concentration is 1 mol/L), continuously carrying out acid washing purification by adopting nitric acid and hydrofluoric acid mixed acid after drying (wherein the acid washing condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the acid washing temperature of the nitric acid and the hydrofluoric acid mixed acid is 25 ℃, the acid washing time of the nitric acid and the hydrofluoric acid mixed acid is 1h, the nitric acid concentration is 1mol/L, and the hydrofluoric acid concentration is 1 mol/L), and drying to obtain the silicon carbide powder. |[0047] The silicon carbide powder prepared in this comparative example has been examined by XRD phase to show that impurity phases such as silicon phase, carbon phase and silicate phase are present in addition to the silicon carbide phase.|[0048] The silicon carbide prepared in this comparative example has excess carbon which is not removed, the purity of the obtained silicon carbide is 72.60%, the recovery rate of the simple substance silicon in the silicon melt refining slag is 68.60%, the granularity D10 of the silicon carbide is 118.67 mu m, the D50 is 353.41 mu m, and the D90 is 788.43 mu m.|[0049] Comparative example 5|Other conditions were identical to example 1 except that:| (5) And (3) directly carrying out pickling purification on the silicon carbide-containing powder obtained in the step (4) by adopting nitric acid and hydrofluoric acid mixed acid (wherein the pickling condition is that the volume ratio of nitric acid to hydrofluoric acid is 3:1, the pickling temperature of the nitric acid and hydrofluoric acid mixed acid is 50 ℃, the pickling time of the nitric acid and hydrofluoric acid mixed acid is 2h, the nitric acid concentration is 3mol/L, and the hydrofluoric acid concentration is 3 mol/L), and drying to obtain the silicon carbide powder. |[0050] The silicon carbide prepared by the comparative example has more silicic acid precipitation during filtration after acid washing and purification of nitric acid and hydrofluoric acid mixed acid, the purity of the obtained silicon carbide is 68.30%, the silicon recycling rate in silicon melt refining slag is 71.50%, the granularity D10 of the silicon carbide is 178.27 mu m, the granularity D50 of the silicon carbide is 393.44 mu m, and the granularity D90 of the silicon carbide is 903.69 mu m.|[0051] While the present invention has been described in detail with reference to the specific embodiments thereof, the present invention is not limited to the above embodiments, and various changes can be made within the knowledge of those skilled in the art without departing from the spirit of the present invention. Family Number|(114287066)|114287066|Abstract|(CN119858921 A)|The invention belongs to the technical field of secondary resource utilization , and relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag . The method realizes value - added recycling of the silicon melt refining slag . The method comprises the following steps : by taking silicon melt refining slag as a silicon source and a waste graphite component as a carbon source , crushing and grinding the silicon melt refining slag and the waste graphite component , adding waste graphite component powder into the silicon melt refining slag according to a weight ratio , uniformly mixing , putting into a high - temperature reaction furnace , and carrying out carbon thermal reduction smelting to prepare a sintered block containing silicon carbide ; then crushing the sintered block containing silicon carbide and carrying out carbon removal treatment in air at different temperatures ; and finally , carrying out acid pickling and drying on the carbon - removed silicon carbide powder to obtain the silicon carbide powder with high additional value . According to the method , the utilization rate of monatomic silicon in the silicon melt refining slag is high , the raw material applicability is high , resources are saved , the prepared silicon carbide is high in quality and uniform in particle size , high - value utilization of the silicon melt refining slag is achieved , and a new direction is provided for disposal of the silicon melt refining slag . |CPC codes|(CN119858921 A)|C01B - 032/984 |C01P - 2004/51 |C01P - 2004/61 |C01P - 2004/62 |C01P - 2006/80 |IPC codes|(CN119858921 A)|C01B - 032/984 | Materials, metallurgy C01B-032/984|C01P-2004/51|C01P-2004/61|C01P-2004/62|C01P-2006/80 C01B-032/984|C01P-2004/51|C01P-2004/61|C01P-2004/62|C01P-2006/80 C01B-032/984 C01B-032/984 CN120348949 CN120348949 115364004 WHO=Examiner SELF=N CAT=A CN118771383|CN112179803|CN109748281|CN108529629|CN118908216 CN118771383 111771142 WHO=Examiner SELF=Y CAT=Y|CN112179803 92191076 WHO=Examiner SELF=Y CAT=Y|CN109748281 84479518 WHO=Examiner SELF=N CAT=Y|CN108529629 81326709 WHO=Examiner SELF=N CAT=Y|CN118908216 112101394 WHO=Examiner SELF=Y CAT=A CN108529629; CN109748281; CN112179803; CN118771383; CN118908216 PENDING (CN119858921)|PENDING ALIVE (CN119858921)|ALIVE (CN119858921)|LEGAL DETAILS FOR CN119858921|Actual or expected expiration date=2045-01-21|Legal state=ALIVE|Status=PENDING|Event publication date=2025-01-21|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510094191|Application date=2025-01-21|Standardized application number=2025CN-0094191|Event publication date=2025-04-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119858921|Publication stage code=A|Publication date=2025-04-22|Standardized publication number=CN119858921|Event publication date=2025-04-22|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-05-09|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN119858921)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSBQv3XXttjClfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000077244201&ekey=1916&xpn=CN119858921&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=8Xf4pcZ8SR50VjODQ%252FG0a5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN119858921)|CN (CN119858921)|NAME=KUNMING UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN119858921)|NAME=JIANG TAIWEI;CHANGSHA RONG ZHI PATENT AGENCY , REG=43114 (CN119858921)|NAME=CHEN ZHENGJIE|NAME=HU YIYOU|NAME=ZHANG YONGHANG|NAME=HU PANPAN|NAME=MA WENHUI|NAME=ZHANG YAKUN 0 1 Titre: (CN119858921)|Regeneration and recovery method of silicon carbide in silicon melt refining slag Résumé: (CN119858921)|The invention belongs to the technical field of secondary resource utilization, and relates to a regeneration and recovery method of silicon carbide in silicon melt refining slag. The method realizes value-added recycling of the silicon melt refining slag. The method comprises the following steps: by taking silicon melt refining slag as a silicon source and a waste graphite component as a carbon source, crushing and grinding the silicon melt refining slag and the waste graphite component, adding waste graphite component powder into the silicon melt refining slag according to a weight ratio, uniformly mixing, putting into a high-temperature reaction furnace, and carrying out carbon thermal reduction smelting to prepare a sintered block containing silicon carbide; then crushing the sintered block containing silicon carbide and carrying out carbon removal treatment in air at different temperatures; and finally, carrying out acid pickling and drying on the carbon-removed silicon carbide powder to obtain the silicon carbide powder with high additional value. According to the method, the utilization rate of monatomic silicon in the silicon melt refining slag is high, the raw material applicability is high, resources are saved, the prepared silicon carbide is high in quality and uniform in particle size, high-value utilization of the silicon melt refining slag is achieved, and a new direction is provided for disposal of the silicon melt refining slag. 92 Abstract gpt-4o-mini no The article focuses on the regeneration and recovery of silicon carbide from silicon melt refining slag, which does not involve accelerated weathering or CO₂ capture.
92 CN201410486205 CN201410486205 CN104313335|CN104313335 68525378 CN104313335 B 2016-09-14 [CN104313335B]|CN104313335 A 2015-01-28 [CN104313335] 2014-09-23 2014-09-23 2016-09-14|2015-01-28 (CN104313335B)|2016-09-14 (CN104313335)|2018-09-23 (CN104313335)|Wet separation and utilization method of ferroalloy manganese dust (CN104313335)|The invention discloses a wet separation utilization method of ferroalloy manganese dust. The method is as below: using water film dedusting wastewater as a reducing agent to conduct carbon removal and alkali metal reduction on ferroalloy manganese dust; extracting by sulfuric acid and FeS2 to obtain manganese sulfate; adding ammonium hydrogen carbonate to produce manganese carbonate and obtain potassium sulfate (potash fertilizer nitrogen); washing the residue from sulfuric acid and FeS2 extraction; extracting with hydrochloric acid; adding ammonium hydrogen carbonate into the extracting solution for reaction to obtain manganese carbonate; concentrating the solution to obtain a snow melting agent; washing, crushing and drying the residue to obtain fine silica powder; and reusing the waste liquid in the production process. The prepared manganese carbonate product has manganese content greater than 43% to increase the Mn content; the potassium oxide content in potassium sulfate is 40-50%; and silicon oxide content in silica powder is 85-95%. The method fully uses ferroalloy manganese dust, does not need the addition of reducing agent, uses the water film dedusting wastewater, improves product quality, increases output, and protects the environment. ZHENG JINGYI ([CN]) (CN104313335)|ZHENG JINGYI ([CN])|(CN104313335)|JILIN FRIEND TECHNOLOGY CO. LTD. ZHENG JINGYI|LÜ WENGUANG (CN104313335)|ZHENG JINGYI|LÜ WENGUANG|(CN104313335)|ZHENG JINGYI|LÜ WENGUANG (CN104313335)|ZHANG TIESHENG;CHANGCHUN DONGSHI PATENT LAW OFFICE|Reg. Nb: 22202 (CN104313335)|The technology of patent equipment authorized by independent intellectual property rights of the inventor is skillfully utilized, so that the process flow has the advantages of saving, reducing consumption, protecting environment, improving efficiency and the like in multiple directions.|However, because the Mn and Zn contents are low, the recycling of the manganese-iron alloy is difficult, the smoke dust and the fine manganese concentrate are mainly mixed and sintered in the industry at present and are returned to a production system for recycling, but the smoke dust loss of the method is large, and the normal furnace condition of the manganese-iron alloy smelting is influenced when the smoke dust is returned for use.|The manganese resources in China are unbalanced in geographical distribution, the ore deposit is small in scale, the mining conditions are poor, the modern industrial technology is difficult to fully utilize for mining, more than 80% of the manganese ore yield comes from local small and medium mines and civil mines, and the yield is difficult to greatly improve.|The types of manganese ores in China are various, the material components are complex, the grade is low, the impurity content is high, the industrial application and the consumption field of the manganese ores with different types and impurities are greatly different or are respectively emphasized, so that millions of tons of high-quality manganese ores must be imported in China every year: firstly, the requirements of China on the production of high-grade manganese ferroalloy, particularly medium-low carbon ferromanganese are met; secondly, the imported ore is matched with domestic ore for use, so that domestic poor manganese oxide ore and poor manganese carbonate ore resources are reasonably and fully utilized, high ore price is integrated, and the raw material cost is reduced; thirdly, the index value of the technical requirement of the charging material is adjusted to achieve the purposes of strengthening smelting, increasing production and reducing consumption, improving the index and producing various grades of manganese alloys economically and reasonably.| (CN104313335)|1. The method for extracting manganese and potassium fertilizer from ferroalloy manganese dust comprises the following steps:mixing iron alloy manganese dust with water film dedusting wastewater, and reacting at 80-120 ℃; scraping carbon on the floating surface to obtain a carbon-removed material, wherein the ratio of the iron alloy manganese dust to the water film dedusting wastewater is 1: 0.9-1.1; reacting for 2 hours; the carbon scraped out is subjected to solid-liquid separation to obtain carbon powder;1) carrying out solid-liquid separation on the materials subjected to the decarbonization to obtain slag 1 and a solution 1;2) adding concentrated sulfuric acid and water into the slag 1, wherein the ratio of the slag to the concentrated sulfuric acid is 1: reacting at a water ratio of 1: 0.9-1.1; performing solid-liquid separation to obtain slag 2 and solution 2;3) mixing solution 1 and solution 2, and adding FeS at a molar ratio of 1-2: 42Carrying out solid-liquid separation after reaction at normal temperature to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates;4) adding ammonium bicarbonate into the solution 3, reacting according to a molar ratio of 1: 0.9-1.1, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate.|6. The wet separating and utilizing process of iron alloy manganese dust includes the following steps:1) carbon removal and alkali metal reduction of iron alloy manganese dust: removing carbon from the ferroalloy manganese dust, and adding a reducing agent to perform a reduction reaction to obtain a material subjected to carbon removal;2) extracting manganese and potassium fertilizer from the ferroalloy manganese dust: performing solid-liquid separation on the decarbonized materials to obtain slag 1 and a solution 1; extracting residue 1 with sulfuric acid, separating solid and liquid to obtain solution 2 and residue 2, mixing solution 1 and solution 2, and adding FeS2After the reaction, carrying out solid-liquid separation to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates; adding ammonium bicarbonate into the solution 3, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate;3) recovering manganese waste residue from the ferroalloy manganese dust by a wet method to extract manganese, a snow-melting agent and silicon dioxide micropowder: a. adding concentrated sulfuric acid into the slag 2 to react with water, and performing solid-liquid separation to obtain slag 3 and a solution 4; b. reacting the residue 3 with 37% hydrochloric acid and water, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5 for reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain a snow-melting agent; c. adding 37% hydrochloric acid into the residue 4 to react with water, and performing solid-liquid separation to obtain residue 5 and solution 6; d, washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;the solution 4 can be reused when the slag 1 is extracted by sulfuric acid; the washing waste water of solution 6 and residue 5 can be used for reacting residue 3 with 37% hydrochloric acid and water.| (CN104313335)|The invention aims to provide a wet separation and utilization method of ferroalloy manganese dust in order to fully utilize manganese dust, improve the value of the manganese dust and reduce the pollution to the environment.|The invention discloses a wet separation and utilization method of ferroalloy manganese dust, which adopts water film dedusting wastewater as a reducing agent to remove carbon and reduce alkali metal from the ferroalloy manganese dust, and adopts sulfuric acid and FeS2Extracting to obtain manganese sulfate, adding ammonium bicarbonate to produce manganese carbonate and potassium sulfate (nitrogen-potassium fertilizer), and adding sulfuric acid and FeS2Washing the extracted residue with sulfuric acid, extracting with hydrochloric acid, adding ammonium bicarbonate into the extractive solution, reacting to obtain manganese carbonate, concentrating the solution to obtain snow-melting agent, washing the residue, pulverizing, and drying to obtain silica micropowder; the waste liquid in the production process is recycled; the manganese content in the obtained manganese carbonate product is more than 43 percent; the content of manganese is increased, and the content of potassium oxide in the potassium sulfate is 40-50 percent; the silicon dioxide micro powder contains 85-95% of silicon oxide.|The invention provides a wet separation and utilization method of ferroalloy manganese dust, which adopts water film dedusting wastewater as a reducing agent to remove carbon and reduce alkali metal from the ferroalloy manganese dust, and adopts sulfuric acid and FeS2Extracting to obtain manganese sulfate, adding ammonium bicarbonate to produce manganese carbonate and potassium sulfate (nitrogen-potassium fertilizer), and adding sulfuric acid and FeS2Washing the extracted residue with sulfuric acid, extracting with hydrochloric acid, adding ammonium bicarbonate into the extractive solution, reacting to obtain manganese carbonate, concentrating the solution to obtain snow-melting agent, washing the residue, pulverizing, and drying to obtain silica micropowder; the waste liquid in the production process is recycled; the manganese content in the obtained manganese carbonate product is more than 43 percent; improveManganese content, potassium oxide content in potassium sulfate 40-50%; the silicon dioxide micro powder contains 85-95% of silicon oxide.| (CN104313335)|FERROALLOY MANGANESE DUST(100,17)|IRON ALLOY(100,17)|EXTRACTING MANGANESE(100,13)|FERROALLOY MANGANESE(100,13)|WET SEPARATION(100,13)|MANGANESE DUST(100,12)|IRON ALLOY MANGANESE DUST(100,10)|POTASSIUM FERTILIZER(100,10)|FERROALLOY MANGANESE UTILIZATION(100,2)|WET SEPARATING(100,2)|FERROALLOY MANGANESE DUST UTILIZATION(67,4)|FILM DEDUSTING WASTEWATER(62,5)|SILICA MICROPOWDER(54,10)|DEBACTEROL(53,25)|HARTSHORN(50,16)|CONCENTRATED DEBACTEROL(43,14)|DOMESTIC POOR OXOMANGANESE(43,1)|EXTRACTION RESIDUE(37,5)|STRENGTHENING SMELTING(36,1)|MANGANESE RESIDUE(35,8)|SLAG(34,39)|METAL SULFIDE PRECIPITATE(33,11)|IMPORTED ORE(33,1)|NITROGEN POTASSIUM FERTILIZER(32,2)|SOLUTION EXTRACTION(32,2)|FINE MANGANESE CONCENTRATE(32,1)|RECOVERING MANGANESE RESIDUE(31,4)|MANGANESE IRON ALLOY SMELTING(31,1)|MANGANESE RESOURCE(31,1)|CIVIL MINE(30,1)|SMOKE DUST(28,5)|MANGANESE FERROALLOY(28,2)|DOMESTIC ORE(28,1)|ORE PRICE(28,1)|ORE RESOURCE(28,1)|SILICA MICRO POWDER(27,10)|ALLOY SMELTING(26,1)|SMOKE DUST LOSS(26,1)|SNOW MELTING(25,15)|WASHING WASTEWATER(25,3)|IMPROVEMANGANESE CONTENT(25,1)|GEOGRAPHICAL DISTRIBUTION(24,1)|WASTE LIQUID(23,2)|POTASSIUM SULFATE(22,13)|IRON ALLOY MANGANESE(22,7)|DOMESTIC POOR(22,1)|SOLUTION WASHING WASTEWATER(21,3)|CONSUMPTION REDUCTION(21,2)|MANGANESE CONTENT(20,8)|RECYCLING(20,2)|MANGANESE II CARBONATE ORE RESOURCE(20,1)|MANGANESE ORE YIELD(20,1)|MANGANESE II CARBONATE(19,24)|ENVIRONMENT PROTECTION(19,1)|MANGANESE DUST VALUE(19,1)|SOLID LIQUID SEPARATION(18,46)|MOLAR RATIO(18,9)|WATER FILM DEDUSTING WASTEWATER(18,6)|MEDIUM MINE(18,1)|MINING CONDITION(18,1)|HYDROGEN CHLORIDE(17,21)|MANGANESE ORE(17,13)|SCRAPING CARBON(17,3)|ZN CONTENT(17,1)|REMOVING CARBON(16,11)|DECARBONIZATION(16,3)|IMPURITY CONTENT(16,2)|MANGANESE IRON ALLOY(15,2)|CONTAMINATION(15,1)|MICRO POWDER(14,10)|POTASSIUM OXIDE CONTENT(14,4)|CRUSHING(13,7)|MIXING SOLUTION(13,6)|IMPURITY(13,1)|ORE DEPOSIT(13,1)|CARBON POWDER(12,3)|FLOATING(12,3)|MANGANESE DEDUSTING ASH(12,3)|CARBON FERROMANGANESE(12,1)|INVENTOR INTELLECTUAL PROPERTY RIGHT(12,1)|SMALL MINE(12,1)|FURNACE(11,1)|SOLID MANGANESE II CARBONATE(10,12)|TON(10,7)|POTASSIUM OXIDE(10,4)|MINING(10,2)|INDUSTRIAL TECHNOLOGY(10,1)|MANGANESE(9,17)|REDUCING AGENT(9,10)|MANGANESE II CARBONATE PRODUCT(9,4)|SOLID SEPARATION(9,4)|MANGANESE ALLOY(9,2)|CHARGING MATERIAL TECHNICAL REQUIREMENT(9,1)|HIGH GRADE MANGANESE FERROALLOY(9,1)|SILICON OXIDE(8,4)|CHARGING MATERIAL(8,1)|HOMELAND RESOURCE MINISTRY(8,1)|ALKALI METAL(7,3)|ORE(7,3)|POTASSIUM ORE RESOURCE(7,2)|WATER RATIO(7,2)|FERROMANGANESE SMELTING DUST(7,1)|INTELLECTUAL PROPERTY RIGHT(6,1)|SULFIDE METALAND PRECIPITATION(6,1)|SUMMER GRAIN HARVEST(6,1)|EXTENSIVE UTILIZATION(5,2)|FLOTATION REAGENT(5,2)|CHINESE MANGANESE INDUSTRY(5,1)|DEBACTEROL LEACHING(5,1)|EQUIPMENT COMPONENT(5,1)|FERROALLOY MANGANESE WET SEPARATION(5,1)|NATIONAL STATISTIC BUREAU(5,1)|OXOMANGANESE MINERAL POWDER(5,1)|POTASH FERTILIZER KILOGRAM(5,1)|PRODUCING VARIOUS GRADE(5,1)|RESOURCE COMPREHENSIVE UTILIZATION(5,1)|RICH MANGANESE ORE RESOURCE(5,1)|WORLD MANGANESE ORE RESOURCE(5,1)|WULAR POTASH FERTILIZER COMPANY(5,1)|ALKALI METAL REDUCTION(4,6)|INORGANIC POWDER(4,3)|PRODUCING MANGANESE SERIES FERROALLOY(4,3)|REDUCTION REACTION(4,3)|FERTILIZER COMPOUND(4,2)|WEIGHT RATIO(4,2)|AGRICULTURAL COUNTRY(4,1)|AGRICULTURE UNIVERSITY(4,1)|FLOTATION EQUIPMENT ADOPTION(4,1)|HIGH QUALITY MANGANESE ORE(4,1)|INTERNATIONAL MANGANESE ORE MARKET(4,1)|MEDIUM LOW CARBON FERROMANGANESE(4,1)|POWDERY WASTE RESIDUE(4,1)|PROCESS FLOW(4,1)|RAW MATERIAL COST(4,1)|REFORM COMMITTEE(4,1)|RESIDUAL SMOKE DUST(4,1)|SMELTING SLAG(4,1)|PRODUCT QUALITY(3,2)|WORLD TOTAL RESERVE(3,2)|APOCYNUM SALT LAKE(3,1)|BIG COUNTRY(3,1)|CARBIDE SLAG(3,1)|CHINA ASSOCIATION(3,1)|CLOTH BAG(3,1)|COAL GANGUE(3,1)|ELECTROLYTIC MANGANESE METAL DEMAND(3,1)|ENVIRONMENT FRIENDLY FLY ASH(3,1)|FERRO MANGANESE DUST(3,1)|FERROALLOY PRODUCTION COUNTRY(3,1)|FOREIGN COUNTRY(3,1)|INDUSTRIAL APPLICATION(3,1)|LEACHING MANGANESE(3,1)|LEAN ORE(3,1)|MANGANESE ACCOUNT(3,1)|MANGANESE ALLOY PRODUCTION(3,1)|MANGANESE ALLOY SMELTING(3,1)|MANGANESE DIOXIDE MINERAL POWDER(3,1)|MANGANESE DIOXIDE ORE POWDER(3,1)|MANGANESE FERROALLOY ELECTRIC FURNACE(3,1)|MANGANESE GRADE(3,1)|MANGANESE ORE RESERVE(3,1)|MANGANESE RICH ORE(3,1)|MANGANESE SERIES FERROALLOY YIELD(3,1)|NATIONAL FERROUS METALLURGY(3,1)|NICKEL SUBSTITUTION(3,1)|POTASSIUM MINERAL(3,1)|REAGENT CONTAMINATION(3,1)|SEA TRANSPORTATION(3,1)|SELLER MARKET(3,1)|SILICATE ROCK(3,1)|SMELTING SMOKE(3,1)|SUMMER GRAIN YIELD(3,1)|TECHNICAL PROCESSABILITY(3,1)|UKRAINE ACCOUNT(3,1)|WET LEACHING(3,1)|GALLIUM(2,3)|INDIUM(2,3)|BLAST FURNACE(2,2)|FOUNDATION(2,2)|GERMANIUM(2,2)|TOTAL MANGANESE(2,2)|ADDING FES(2,1)|COMMERCIALLY VALUABLE MANGANESE ORE(2,1)|COMPLEX MANGANESE(2,1)|DEVELOPMENT STATE(2,1)|EQUIPMENT CORROSION(2,1)|FERTILIZATION STANDARD(2,1)|GENERATED SMOKE DUST(2,1)|H2SO MASS FRACTION(2,1)|MN CONTENT(2,1)|POTASSIUM SULFATE COMPOUND FERTILIZER(2,1)|PRODUCTION SYSTEM(2,1)|SCRAPED CARBON(2,1)|TARIFF REASON(2,1)|TECHNOLOGICAL CONDITION(2,1)|ACCOUNTING(1,1)|ADSORBENT(1,1)|ALLOY MANUFACTURER(1,1)||(CN104313335)|IRON ALLOY(100,19)|FERROALLOY MANGANESE DUST(100,17)|SNOW MELTING(100,15)|EXTRACTING MANGANESE(100,13)|FERROALLOY MANGANESE(100,13)|MANGANESE DUST(100,13)|WET SEPARATION(100,12)|IRON ALLOY MANGANESE DUST(100,11)|POTASSIUM FERTILIZER(100,10)|SILICA MICROPOWDER(100,10)|CARBON(100,9)|ALKALI METAL REDUCTION(100,8)|MANGANESE RESIDUE(100,8)|WET(100,4)|FERROALLOY MANGANESE UTILIZATION(100,3)|WET SEPARATING(100,2)|FERROALLOY MANGANESE DUST UTILIZATION(63,4)|FILM DEDUSTING WASTEWATER(59,5)|NITROGENOUS POTASH FERTILIZER(59,2)|DEBACTEROL(52,25)|HARTSHORN(50,16)|CONCENTRATED DEBACTEROL(48,14)|DOMESTIC POOR OXOMANGANESE(41,1)|SLAG(37,39)|EXTRACTION RESIDUE(35,5)|STRENGTHENING SMELTING(34,1)|METAL SULFIDE PRECIPITATE(31,12)|IMPORTED ORE(31,1)|SOLUTION EXTRACTION(30,2)|FINE MANGANESE CONCENTRATE(30,1)|RECOVERING MANGANESE RESIDUE(29,4)|CIVIL MINE(29,1)|MANGANESE IRON ALLOY SMELTING(29,1)|MANGANESE RESOURCE(29,1)|SILICA MICRO POWDER(28,10)|DOMESTIC ORE(27,1)|ORE PRICE(27,1)|ORE RESOURCE(27,1)|SMOKE DUST(26,5)|MANGANESE FERROALLOY(26,2)|ALLOY SMELTING(25,1)|SMOKE DUST LOSS(25,1)|WASHING WASTEWATER(24,3)|WASTE LIQUID(22,2)|GEOGRAPHICAL DISTRIBUTION(22,1)|POTASSIUM SULFATE(21,13)|IRON ALLOY MANGANESE(21,8)|DOMESTIC POOR(21,1)|SOLUTION WASHING WASTEWATER(20,3)|CONSUMPTION REDUCTION(20,2)|SOLID LIQUID SEPARATION(19,46)|MOLAR RATIO(19,9)|RECYCLING(19,2)|SCRAPED CARBON(19,2)|MANGANESE II CARBONATE ORE RESOURCE(19,1)|MANGANESE ORE YIELD(19,1)|HYDROGEN CHLORIDE(18,21)|MANGANESE CONTENT(18,9)|ENVIRONMENT PROTECTION(18,1)|MANGANESE DUST VALUE(18,1)|REMOVING CARBON(17,12)|MEDIUM MINE(17,1)|MINING CONDITION(17,1)|MANGANESE II CARBONATE(16,22)|MANGANESE ORE(16,13)|DECARBONIZATION(16,3)|SCRAPING CARBON(16,3)|ZN CONTENT(16,1)|MICRO POWDER(15,10)|CRUSHING(15,7)|IMPURITY CONTENT(15,2)|MANGANESE CARBONATE(15,1)|POTASSIUM OXIDE CONTENT(14,4)|MANGANESE IRON ALLOY(14,2)|CONTAMINATION(14,1)|MIXING SOLUTION(13,6)|WATER FILM DEDUSTING WASTEWATER(12,6)|CARBON POWDER(12,3)|IMPURITY(12,1)|ORE DEPOSIT(12,1)|SOLID MANGANESE II CARBONATE(11,12)|FLOATING(11,3)|MANGANESE DEDUSTING ASH(11,3)|CARBON FERROMANGANESE(11,1)|FURNACE(11,1)|INVENTOR INTELLECTUAL PROPERTY RIGHT(11,1)|SMALL MINE(11,1)|MINING(10,2)|FES(10,1)|TON(9,7)|POTASSIUM OXIDE(9,4)|SOLID SEPARATION(9,4)|MANGANESE ALLOY(9,2)|CHARGING MATERIAL TECHNICAL REQUIREMENT(9,1)|HIGH GRADE MANGANESE FERROALLOY(9,1)|INDUSTRIAL TECHNOLOGY(9,1)|MANGANESE(8,17)|REDUCING AGENT(8,10)|MANGANESE II CARBONATE PRODUCT(8,4)|SILICON OXIDE(8,4)|CHARGING MATERIAL(8,1)|HOMELAND RESOURCE MINISTRY(8,1)|ALKALI METAL(7,3)|ORE(7,3)|WATER RATIO(7,2)|WEIGHT RATIO(7,2)|POTASSIUM ORE RESOURCE(6,2)|FERROMANGANESE SMELTING DUST(6,1)|INTELLECTUAL PROPERTY RIGHT(6,1)|SUMMER GRAIN HARVEST(6,1)|EXTENSIVE UTILIZATION(5,2)|FLOTATION REAGENT(5,2)|NATIONAL STATISTIC BUREAU(5,1)|RESOURCE COMPREHENSIVE UTILIZATION(5,1)|WULAR POTASH FERTILIZER COMPANY(5,1)|INORGANIC POWDER(4,3)|PRODUCING MANGANESE SERIES FERROALLOY(4,3)|REDUCTION REACTION(4,3)|AGRICULTURAL COUNTRY(4,1)|AGRICULTURE UNIVERSITY(4,1)|CHINESE MANGANESE INDUSTRY(4,1)|DEBACTEROL LEACHING(4,1)|EQUIPMENT COMPONENT(4,1)|FLOTATION EQUIPMENT ADOPTION(4,1)|HIGH QUALITY MANGANESE ORE(4,1)|INTERNATIONAL MANGANESE ORE MARKET(4,1)|MEDIUM LOW CARBON FERROMANGANESE(4,1)|OXOMANGANESE MINERAL POWDER(4,1)|POTASH FERTILIZER KILOGRAM(4,1)|POWDERY WASTE RESIDUE(4,1)|PROCESS FLOW(4,1)|PRODUCING VARIOUS GRADE(4,1)|RAW MATERIAL COST(4,1)|REFORM COMMITTEE(4,1)|RESIDUAL SMOKE DUST(4,1)|RICH MANGANESE ORE RESOURCE(4,1)|SMELTING SLAG(4,1)|WORLD MANGANESE ORE RESOURCE(4,1)|FERTILIZER COMPOUND(3,2)|PRODUCT QUALITY(3,2)|WORLD TOTAL RESERVE(3,2)|APOCYNUM SALT LAKE(3,1)|BIG COUNTRY(3,1)|CARBIDE SLAG(3,1)|CHINA ASSOCIATION(3,1)|CLOTH BAG(3,1)|COAL GANGUE(3,1)|ELECTROLYTIC MANGANESE METAL DEMAND(3,1)|ENVIRONMENT FRIENDLY FLY ASH(3,1)|FERRO MANGANESE DUST(3,1)|FERROALLOY PRODUCTION COUNTRY(3,1)|FOREIGN COUNTRY(3,1)|INDUSTRIAL APPLICATION(3,1)|LEACHING MANGANESE(3,1)|LEAN ORE(3,1)|MANGANESE ACCOUNT(3,1)|MANGANESE ALLOY PRODUCTION(3,1)|MANGANESE ALLOY SMELTING(3,1)|MANGANESE DIOXIDE MINERAL POWDER(3,1)|MANGANESE DIOXIDE ORE POWDER(3,1)|MANGANESE FERROALLOY ELECTRIC FURNACE(3,1)|MANGANESE GRADE(3,1)|MANGANESE ORE RESERVE(3,1)|MANGANESE RICH ORE(3,1)|MANGANESE SERIES FERROALLOY YIELD(3,1)|NATIONAL FERROUS METALLURGY(3,1)|NICKEL SUBSTITUTION(3,1)|POTASSIUM MINERAL(3,1)|REAGENT CONTAMINATION(3,1)|SEA TRANSPORTATION(3,1)|SELLER MARKET(3,1)|SILICATE ROCK(3,1)|SMELTING SMOKE(3,1)|SUMMER GRAIN YIELD(3,1)|TECHNICAL PROCESSABILITY(3,1)|UKRAINE ACCOUNT(3,1)|WET LEACHING(3,1)|GALLIUM(2,3)|INDIUM(2,3)|BLAST FURNACE(2,2)|FOUNDATION(2,2)|GERMANIUM(2,2)|TOTAL MANGANESE(2,2)|ADDING FES(2,1)|COMMERCIALLY VALUABLE MANGANESE ORE(2,1)|COMPLEX MANGANESE(2,1)|DEVELOPMENT STATE(2,1)|EQUIPMENT CORROSION(2,1)|FERTILIZATION STANDARD(2,1)|GENERATED SMOKE DUST(2,1)|H2SO MASS FRACTION(2,1)|MN CONTENT(2,1)|POTASSIUM SULFATE COMPOUND FERTILIZER(2,1)|PRODUCTION SYSTEM(2,1)|TARIFF REASON(2,1)|TECHNOLOGICAL CONDITION(2,1)|ACCOUNTING(1,1)|ADSORBENT(1,1)|ALLOY MANUFACTURER(1,1)|ANIMAL HUSBANDRY(1,1)| (CN104313335)|1. The method for extracting manganese and potassium fertilizer from ferroalloy manganese dust comprises the following steps:|mixing iron alloy manganese dust with water film dedusting wastewater, and reacting at 80-120 ℃; scraping carbon on the floating surface to obtain a carbon-removed material, wherein the ratio of the iron alloy manganese dust to the water film dedusting wastewater is 1: 0.9-1.1; reacting for 2 hours; the carbon scraped out is subjected to solid-liquid separation to obtain carbon powder;|1) carrying out solid-liquid separation on the materials subjected to the decarbonization to obtain slag 1 and a solution 1;|2) adding concentrated sulfuric acid and water into the slag 1, wherein the ratio of the slag to the concentrated sulfuric acid is 1: reacting at a water ratio of 1: 0.9-1.1; performing solid-liquid separation to obtain slag 2 and solution 2;|3) mixing solution 1 and solution 2, and adding FeS at a molar ratio of 1-2: 42Carrying out solid-liquid separation after reaction at normal temperature to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates;|4) adding ammonium bicarbonate into the solution 3, reacting according to a molar ratio of 1: 0.9-1.1, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate.|2. The method for extracting manganese and potassium fertilizers from ferroalloy manganese dust according to claim 1, wherein the method comprises the following steps: the reaction in the step 2) is that the slag 1 reacts with concentrated sulfuric acid firstly, and then water is added for continuous reaction.|3. The method for extracting manganese and potassium fertilizers from ferroalloy manganese dust according to claim 1 or 2, wherein the method comprises the following steps: the concentration of the concentrated sulfuric acid is 90%; step 4) the reaction time was 4 hours.|4. The method for extracting manganese, snow-melting agent and silicon dioxide micropowder from manganese waste residue recovered by ferroalloy manganese dust wet process comprises the following steps:|1) the slag 2 of claim 1, enriched with sulfuric acid and water, as slag 2: concentrated sulfuric acid: reacting water = 1: 0.4-0.6: 1, and performing solid-liquid separation to obtain residue 3 and solution 4;|2) adding 37% hydrochloric acid and water into residue 3, and mixing the following materials: acid: reacting water = 1: 0.35-0.45: 1, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5, reacting at a molar ratio of 1: 0.9-1.1, performing solid-liquid separation to obtain solid manganese carbonate, concentrating the liquid, and drying to obtain snow-melting agent;|3) adding 37% hydrochloric acid and water into the residue 4, and mixing the materials according to the weight ratio of the residue 4: hydrochloric acid: reacting water = 1: 0.15-0.25: 1, and performing solid-liquid separation to obtain residue 5 and solution 6;|4) washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;|the concentrated sulfuric acid is more than 70 percent.|5. The method for extracting manganese, a snow-melting agent and silicon dioxide micropowder from manganese waste residue recovered by the ferroalloy manganese dust wet method according to claim 4, which is characterized by comprising the following steps: the reaction in the step 1) is that the slag 2 reacts with concentrated sulfuric acid firstly, and then water is added for continuous reaction; the reaction in the step 2) is to react with hydrochloric acid firstly and then add water for continuous reaction;|the concentrated sulfuric acid is more than 90 percent.|6. The wet separating and utilizing process of iron alloy manganese dust includes the following steps:|1) carbon removal and alkali metal reduction of iron alloy manganese dust: removing carbon from the ferroalloy manganese dust, and adding a reducing agent to perform a reduction reaction to obtain a material subjected to carbon removal;|2) extracting manganese and potassium fertilizer from the ferroalloy manganese dust: performing solid-liquid separation on the decarbonized materials to obtain slag 1 and a solution 1; extracting residue 1 with sulfuric acid, separating solid and liquid to obtain solution 2 and residue 2, mixing solution 1 and solution 2, and adding FeS2After the reaction, carrying out solid-liquid separation to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates; adding ammonium bicarbonate into the solution 3, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate;|3) recovering manganese waste residue from the ferroalloy manganese dust by a wet method to extract manganese, a snow-melting agent and silicon dioxide micropowder: a. adding concentrated sulfuric acid into the slag 2 to react with water, and performing solid-liquid separation to obtain slag 3 and a solution 4; b. reacting the residue 3 with 37% hydrochloric acid and water, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5 for reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain a snow-melting agent; c. adding 37% hydrochloric acid into the residue 4 to react with water, and performing solid-liquid separation to obtain residue 5 and solution 6; d, washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;|the solution 4 can be reused when the slag 1 is extracted by sulfuric acid; the washing waste water of solution 6 and residue 5 can be used for reacting residue 3 with 37% hydrochloric acid and water.|7. The method for separating and utilizing ferroalloy manganese dust by a wet method according to claim 6, wherein the method comprises the following steps: step 1), step 2) is the method of claim 1; step 3) is the method of claim 4. (CN104313335)|TECHNICAL FIELD|[0002] The invention belongs to the technical field of metallurgy, and particularly relates to a wet separation and utilization method of ferroalloy manganese dust.|BACKGROUND ART|[0004] Manganese ore is an important basic bulk raw material mineral product for the industrial industry. Manganese is the most basic element of steel, and is an alloying element which has important influence on the performance of steel and steel products thereof, and all steel grades and steel products thereof contain manganese. Manganese is widely distributed in nature in many forms, and almost all kinds of ores and silicate rocks contain manganese minerals. The primary products of manganese ore comprise manganese ore for metallurgy, manganese carbonate mineral powder, manganese dioxide mineral powder for chemical industry, manganese oxide mineral powder for batteries and the like. The metallurgical industry is the largest of manganese ores|[0005] The main uses of the alloy are deoxidant and desulfurizer for iron making and steel making, and alloy manufacturing, more than 90% of the total output of manganese ore is used for producing manganese series ferroalloy in the world. China is a big country for producing manganese series ferroalloy and manganese metal, and the yield of the manganese series ferroalloy is more than 445 million tons. After the process for producing stainless steel by substituting nickel with manganese breaks through, the demand of electrolytic manganese metal is increased dramatically, and the yield of the electrolytic manganese metal is 60 ten thousand tons. The amount of the manganese ore used for metallurgy is more than 1000 ten thousand tons every year. Manganese accounts for about 3% of the total manganese used in the battery industry, and the amount of manganese used in the chemical industry (manganese dioxide ore powder is used as an oxidant and used for preparing manganese dioxide, manganese sulfate, potassium permanganate, manganese carbonate, manganese nitrate, manganese chloride and the like) accounts for about 2% of the total manganese; about 5% of manganese ore resources are used in other industries such as the light industry (matches, paints, soaps), the building material industry (colorants and discolorants for glass, ceramics and enamels), the electronics industry (magnetic materials), the environmental protection (adsorbents), the farming and animal husbandry (compound fertilizers, compound feeds) and the defense industry.|[0006] The worldwide-available and commercially-valuable manganese ore reserves are about 9-10 million tons, the global manganese metal distribution is obviously unbalanced, south africa and ukraine are two countries with the largest total amount of manganese ore resources in the world, the south africa manganese ore resources account for about 71.8 percent of the world manganese ore resources, and the ukraine accounts for 11.9 percent, wherein the four countries with the top-ranked world basic reserves account for 92.88 percent of the world total reserves.|[0007] The manganese resources in China are unbalanced in geographical distribution, the ore deposit is small in scale, the mining conditions are poor, the modern industrial technology is difficult to fully utilize for mining, more than 80% of the manganese ore yield comes from local small and medium mines and civil mines, and the yield is difficult to greatly improve. Meanwhile, the lean ores are more, the manganese-rich ores are less, the ore grade is low, the impurity content is high, the granularity is fine, the technical processability is poor, and the requirement of producing manganese series ferroalloy in China cannot be met. Moreover, the guarantee period of the existing manganese ore reserves is only 12 years.|[0008] At present, over ten countries abroad produce manganese ores, wherein the high-grade manganese ores are mainly produced in south Africa, Australia and galbanum, and the grade of manganese in the ores is generally 44-52%; the international manganese ore market is often in a state of short supply and short demand, basically is a seller market, and countries with rich manganese ore resources almost monopolize the pricing right of manganese ore.|[0009] Currently, the manganese-based alloy production in China is 745 million tons (excluding electrolytic manganese metal) as the largest manganese-based ferroalloy producing country in the world. The types of manganese ores in China are various, the material components are complex, the grade is low, the impurity content is high, the industrial application and the consumption field of the manganese ores with different types and impurities are greatly different or are respectively emphasized, so that millions of tons of high-quality manganese ores must be imported in China every year: firstly, the requirements of China on the production of high-grade manganese ferroalloy, particularly medium-low carbon ferromanganese are met; secondly, the imported ore is matched with domestic ore for use, so that domestic poor manganese oxide ore and poor manganese carbonate ore resources are reasonably and fully utilized, high ore price is integrated, and the raw material cost is reduced; thirdly, the index value of the technical requirement of the charging material is adjusted to achieve the purposes of strengthening smelting, increasing production and reducing consumption, improving the index and producing various grades of manganese alloys economically and reasonably.|[0010] The national development and reform committee "guide opinions on the comprehensive utilization of resources and notice of the comprehensive utilization embodiment of bulk solid waste" (issue modification ring fundamentals [2011] 2919) "defines" bulk industrial solid waste "as: the method refers to solid waste which is produced by more than 1,000 million tons in production activities in various industrial fields of China and has great influence on environment and safety, and mainly comprises the following steps: tailings, coal gangue, fly ash, smelting slag, industrial by-product gypsum, red mud and carbide slag.|[0011] The ferro-manganese dust of the ferro-manganese alloy is also called as smoke dust of ferromanganese smelting, is industrial powdery waste residue obtained by collecting dust generated by smoke dust generated in the process of producing the ferro-manganese alloy by high-temperature reduction with an electric furnace method, mainly contains elements such as iron, manganese, zinc, potassium and the like, and is a good secondary resource. However, because the Mn and Zn contents are low, the recycling of the manganese-iron alloy is difficult, the smoke dust and the fine manganese concentrate are mainly mixed and sintered in the industry at present and are returned to a production system for recycling, but the smoke dust loss of the method is large, and the normal furnace condition of the manganese-iron alloy smelting is influenced when the smoke dust is returned for use.|[0012] The ferroalloy manganese dust contains manganese 17-30%, potassium 5-20%, silicon dioxide 20-50%, carbon 1-5%, and also contains lithium, indium, gallium, germanium, zinc, lead, etc.|[0013] The manganese dedusting ash is manganese ore for metallurgy (YB/T319-2005) of a manganese mine according to the national ferrous metallurgy industry standard, and the manganese content of the manganese dedusting ash reaches B class and partially reaches A class.|[0014] The dedusting ash is used as sintering material to be put into the blast furnace again, but the sintering material brings great problems to the production of the blast furnace due to the rich alkali metals (potassium, sodium) and the like. The reuse causes the alkali metal to severely corrode equipment.|[0015] The literature, experimental research on leaching manganese from manganese dedusting ash (the Chinese manganese industry, 2 nd 2011), introduces the principle and process conditions of manganese series alloy smelting smoke dust wet leaching. Under certain technological conditions, pyrite is used as a reducing agent, manganese alloy smelting smoke dust with the Mn content of 28.95% is directly leached out by sulfuric acid, and the leaching rate reaches 93.22%.|[0016] In the document, manganese is extracted from manganese-based ferroalloy electric furnace environment-friendly fly ash containing complex manganese phases by a wet method, and more than 85% of manganese can be recovered.|[0017] In the experimental research on leaching of manganese and zinc from ferromanganese smelting smoke dust in the literature (the 5 th stage in 2014 of the chemical engineering progress), ferromanganese smelting smoke dust is used as a raw material, FeSO4.7H2O is used as a reducing agent, manganese and zinc elements enter a solution in the forms of Mn2+ and Zn2+ through sulfuric acid leaching, and the manganese and zinc elements are separated and extracted. Research shows that the optimal process conditions for leaching are as follows: the mass fraction of H2SO4 is 20%, the reaction time is 4H, the reaction temperature is 90 ℃, the liquid-solid ratio is 5: 1, the adding amount of reducing agent FeSO4.7H2O is 75g, and the stirring speed is 300 r/min. The leaching rate of manganese can reach 96.76 percent, and the leaching rate of zinc is 84.88 percent.|[0018] Traditionally, flotation equipment and flotation reagents (reducing agents) are adopted to select carbon, so that the environment and rear-end products are polluted.|[0019] The results of experiments on the potassium fertilizer application amount and the yield increase effect of rice in 10 provinces of China ever by the university of agriculture show that: according to the current fertilization standard, one kilogram of potash fertilizer is applied to each mu, and the yield of grains can be increased by 4-6 kilograms. Potash fertilizers also increase crop resistance to drought, frost and disease. According to data published by the national statistical bureau, the yield of summer grain in China is 2638 jin this year, and is increased by 39 jin compared with the yield in the last year, and the harvest of the summer grain is continuously realized in the 10 th year. This is greatly related to the amount of potash fertilizer in our country.|[0020] Data provided by the china association for inorganic salts show: nearly 700 million tons of potash fertilizer are imported from foreign countries every year in China. While the potassium minerals in the world are mainly in canada and russia, accounting for 46.3% and 34.7% of the world's total reserves, respectively. For transportation and tariff reasons, China mainly imports potash fertilizers from Russia. Among them, the Wular potash fertilizer company delivers about 250 ten thousand tons of potash fertilizer to China through railways and sea transportation every year.|[0021] The reserve of Chinese sylvite only accounts for 2.36% of the total reserve in the world, the reserve is mainly concentrated in the Qinghai Kao er salt lake and the Xinjiang Apocynum salt lake, and the mining quantities of the two mining areas are close to the limit. In 2010, the ministry of homeland resources determined that potassium salt is one of 8 bulk minerals in short supply in China.|[0022] At present, potassium ore resources are not only deficient in China, but also in agricultural countries such as the United states, Brazil, India and the like, and the competition for potassium ore resources in future is global.|DISCLOSURE|[0023] Disclosure of Invention|[0024] The invention aims to provide a wet separation and utilization method of ferroalloy manganese dust in order to fully utilize manganese dust, improve the value of the manganese dust and reduce the pollution to the environment.|[0025] The carbon removing and alkali metal reducing process of iron alloy manganese dust includes the following steps: mixing iron alloy manganese dust with water film dedusting wastewater, and reacting at 80-120 ℃; scraping carbon on the floating surface to obtain a carbon-removed material; the carbon scraped out is subjected to solid-liquid separation to obtain carbon powder;|[0026] the ratio of the iron alloy manganese dust to the water film dedusting wastewater is 1: 0.9-1.1; the reaction was carried out for 2 hours.|[0027] Method for extracting manganese and potassium fertilizer from iron alloy manganese dust|[0028] 1) Carrying out solid-liquid separation on the materials subjected to the decarbonization to obtain slag 1 and a solution 1;|[0029] 2) adding concentrated sulfuric acid and water into the slag 1, wherein the ratio of the slag to the concentrated sulfuric acid is 1: reacting at a water ratio of 1: 0.9-1.1; performing solid-liquid separation to obtain slag 2 and solution 2;|[0030] 3) mixing solution 1 and solution 2, and adding FeS at a molar ratio of 1-2: 42Carrying out solid-liquid separation after reaction at normal temperature to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates;|[0031] 4) adding ammonium bicarbonate into the solution 3, reacting at a molar ratio of 1: 0.9-1.1, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate;|[0032] the reaction in the step 2 is that the slag 1 reacts with concentrated sulfuric acid firstly, and then water is added for continuous reaction;|[0033] the concentration of the concentrated sulfuric acid is 90%;|[0034] step 4 the reaction time was 4 hours.|[0035] The method for extracting manganese, snow-melting agent and silicon dioxide micropowder from manganese waste residue recovered by ferroalloy manganese dust wet process comprises the following steps:|[0036] 1) adding concentrated sulfuric acid and water into the slag 2, and mixing the slag 2: concentrated sulfuric acid: reacting water = 1: 0.4-0.6: 1, and performing solid-liquid separation to obtain residue 3 and solution 4;|[0037] 2) adding 37% hydrochloric acid and water into residue 3, and mixing the following materials: acid: reacting water = 1: 0.35-0.45: 1, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5, reacting at a molar ratio of 1: 0.9-1.1, performing solid-liquid separation to obtain solid manganese carbonate, concentrating the liquid, and drying to obtain snow-melting agent;|[0038] 3) adding 37% hydrochloric acid and water into the residue 4, and mixing the materials according to the weight ratio of the residue 4: hydrochloric acid: reacting water = 1: 0.15-0.25: 1, and performing solid-liquid separation to obtain residue 5 and solution 6; .|[0039] 4) Washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;|[0040] the concentrated sulfuric acid is more than 70 percent.|[0041] The reaction in the step 1 is that the slag 2 reacts with concentrated sulfuric acid firstly, and then water is added for continuous reaction; the reaction in the step 2 is to react with hydrochloric acid firstly and then add water for continuous reaction.|[0042] The concentrated sulfuric acid is more than 90 percent.|[0043] The wet separating and utilizing process of iron alloy manganese dust includes the following steps:|[0044] 1) carbon removal and alkali metal reduction of iron alloy manganese dust: removing carbon from the ferroalloy manganese dust, and adding a reducing agent to perform a reduction reaction to obtain a material subjected to carbon removal;|[0045] 2) extracting manganese and potassium fertilizer from the ferroalloy manganese dust: performing solid-liquid separation on the decarbonized materials to obtain slag 1 and a solution 1; extracting residue 1 with sulfuric acid, separating solid and liquid to obtain solution 2 and residue 2, mixing solution 1 and solution 2, and adding FeS2After the reaction, carrying out solid-liquid separation to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates; adding ammonium bicarbonate into the solution 3, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate;|[0046] 3) recovering manganese waste residue from ferroalloy manganese dust by a wet method to extract manganese, a snow-melting agent and silicon dioxide micropowder, adding concentrated sulfuric acid into the residue 2 to react with water, and performing solid-liquid separation to obtain residue 3 and solution 4; b. reacting the residue 3 with 37% hydrochloric acid and water, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5 for reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain a snow-melting agent; c. adding 37% hydrochloric acid into the residue 4 to react with water, and performing solid-liquid separation to obtain residue 5 and solution 6; d, washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;|[0047] the solution 4 can be reused when the slag 1 is extracted by sulfuric acid; the washing waste water of solution 6 and residue 5 can be used for reacting residue 3 with 37% hydrochloric acid and water.|[0048] The method for removing carbon and reducing alkali metal from the iron alloy manganese dust, the method for extracting manganese and potash fertilizer from the iron alloy manganese dust, and the method for recovering manganese waste residue by using the wet method from the iron alloy manganese dust to extract manganese, a snow melting agent and silicon dioxide micropowder can be respectively adopted in the steps 1), 2) and 3).|[0049] The invention provides a wet separation and utilization method of ferroalloy manganese dust, which adopts water film dedusting wastewater as a reducing agent to remove carbon and reduce alkali metal from the ferroalloy manganese dust, and adopts sulfuric acid and FeS2Extracting to obtain manganese sulfate, adding ammonium bicarbonate to produce manganese carbonate and potassium sulfate (nitrogen-potassium fertilizer), and adding sulfuric acid and FeS2Washing the extracted residue with sulfuric acid, extracting with hydrochloric acid, adding ammonium bicarbonate into the extractive solution, reacting to obtain manganese carbonate, concentrating the solution to obtain snow-melting agent, washing the residue, pulverizing, and drying to obtain silica micropowder; the waste liquid in the production process is recycled; the manganese content in the obtained manganese carbonate product is more than 43 percent; improveManganese content, potassium oxide content in potassium sulfate 40-50%; the silicon dioxide micro powder contains 85-95% of silicon oxide. The iron alloy manganese dust is fully utilized; no reducing agent is added, water film dedusting wastewater is utilized, product quality is improved, output value is increased, and environment is protected.|[0050] The invention is characterized in that:|[0051] 1. the carbon in the fly ash is floated by steam (according to the special physical structure characteristics of the fly ash); compared with the traditional method of adopting flotation equipment and flotation reagent to select carbon, the method avoids reagent pollution on rear-end products, saves investment and production cost and obtains unexpected effects;|[0052] 2. the water film dedusting wastewater (absorbing reducing substances such as sulfite and the like generated by flue gas) is utilized to dissolve alkali metals (potassium and sodium) in the dedusting ash, and meanwhile, a foundation is laid for the reduction of high-valence manganese, and an unexpected effect is obtained;|[0053] 3. manganese carbonate, silicon dioxide micro powder, potassium sulfate compound fertilizer, environment-friendly snow-melting agent (calcium magnesium potassium chloride) and rare noble metal (nickel, cobalt, indium, gallium, germanium, zinc and lead) compounds are separated and extracted from the dust removal ash, and comprehensive utilization is realized in all directions without precedent.|[0054] 4. The technology of patent equipment authorized by independent intellectual property rights of the inventor is skillfully utilized, so that the process flow has the advantages of saving, reducing consumption, protecting environment, improving efficiency and the like in multiple directions.|DRAWINGS DESCRIPTION|[0056] FIG. 1 is a flow chart of the wet separation and utilization method of ferroalloy manganese dust.|INVENTION MODE|[0057] Detailed Description|INVENTION MODE|[0058] Example 1 method for removing carbon from iron alloy manganese dust and reducing alkali metal|[0059] The manganese-iron alloy is produced by high-temperature reduction in an electric furnace method, the generated smoke dust is collected by a cloth bag method; and the residual smoke dust is dedusted by a water film deduster, and water film dedusting wastewater is collected.|[0060] The solid-liquid ratio of the iron alloy manganese dust to the water film dedusting wastewater is 1: 1, mixing, introducing water vapor to ensure that the temperature of a reaction system is 80-120 ℃; a drum type reaction tank (ZL 200820072919.1) with a grinding device was used for 2 hours of reaction. Scraping carbon on the floating surface to obtain a carbon-removed material; and (3) carrying out solid-liquid separation on the scraped carbon by adopting an inorganic salt precipitate continuous washing machine (ZL 200920093696.1) to obtain carbon powder. This decarburizing process. Meanwhile, the water film dedusting wastewater (absorbing reducing substances such as sulfite generated by flue gas) is utilized to dissolve alkali metals (potassium and sodium) in the dedusting ash, and a foundation is laid for reducing high-valence manganese.|[0061] The ferro-alloy manganese dust is smoke dust generated in the process of producing ferro-manganese alloy by high-temperature reduction with an electric furnace method and collected by a dry method or a warm method.|[0062] The water film dedusting wastewater is the wastewater generated in the water film dedusting process in the process of producing ferromanganese alloy by high-temperature reduction with an electric furnace method|INVENTION MODE|[0063] Example 2 method for extracting manganese and potassium fertilizers from ferroalloy manganese dust|[0064] 1. Carrying out solid-liquid separation on the materials subjected to carbon removal in the embodiment 1 to obtain slag 1 and a solution 1;|[0065] 2. adding concentrated sulfuric acid and water into the slag 1, wherein the slag 1: concentrated sulfuric acid: the proportion of water is 1: 1: 1, the reaction was carried out using a drum type reaction tank (ZL 200820072919.1) equipped with a polishing apparatus. After 2 hours of reaction; performing solid-liquid separation to obtain slag 2 and solution 2;|[0066] 3. mixing solution 1 and solution 2, adding FeS2,FeS2Mixing with the mixed solution (molar ratio 1-2: 4) of solution 1 and solution 2, reacting at room temperature, and performing solid-liquid separation to obtain solution 3 and sulfide metal precipitate (nickel, cobalt, indium, gallium, zinc, and lead), which is formed by precipitation of sulfide metalAnd (4) concentrating wet separation.|[0067] 4. Adding ammonium bicarbonate (molar ratio 1: 1) into the solution 3 for reaction, after 4 hours of reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying potassium sulfate (nitrogen-containing potassium fertilizer) from the liquid.|INVENTION MODE|[0068] Example 3 method for extracting manganese, snow-melting agent and silica micropowder from manganese waste residue recovered from ferroalloy manganese dust by wet process.|[0069] 1. Adding concentrated sulfuric acid (material: concentrated sulfuric acid: water = 1: 0.5: 1) into the slag 2 for reaction, and carrying out solid-liquid separation to obtain slag 3 and a solution 4; the solution 4 can be returned to the slag 1 for utilization. The concentrated sulfuric acid concentration is more than 70%.|[0070] 2. Adding 37% hydrochloric acid (material: acid: water = 1: 0.4: 1) into the residue 3 for reaction, and carrying out solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5 for reaction (the molar ratio is 1: 1), after 4 hours of reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain a snow-melting agent (calcium magnesium potassium chloride composite salt);|[0071] 3. adding 37% hydrochloric acid (material: acid: water = 1: 0.2: 1) into the residue 4 for reaction, and performing solid-liquid separation to obtain residue 5 and solution 6; the solution 6 can be returned to the slag 3 for use.|[0072] 4. Washing the slag 5 with water (ZL 201120091074.2), separating solid and liquid, returning the solution 7 to the slag 3, washing the slag 5 with an inorganic salt precipitate continuous washing machine (ZL 200920093696.1), and crushing and drying the slag by a drying and crushing all-in-one machine (ZL 200920093766.3) to obtain the silicon dioxide micropowder.|[0073] The manganese content in the obtained manganese carbonate product is more than 43 percent; the manganese content in the manganese sulfate product produced by the existing method is more than 31 percent; the potassium oxide content in the potassium sulfate product is 40-50%; the silicon dioxide micro powder contains 85-95% of silicon oxide.|INVENTION MODE|[0074] Example 4 wet separation of ferroalloy manganese dust using method 1) decarbonization and alkali metal reduction of ferroalloy manganese dust: removing carbon from the ferroalloy manganese dust, and adding a reducing agent to perform a reduction reaction to obtain a material subjected to carbon removal;|[0075] 2) extracting manganese and potassium fertilizer from the ferroalloy manganese dust; carrying out solid-liquid separation on the decarbonized materials to obtain slag 1 and a solution 1; extracting residue 1 with sulfuric acid, separating solid and liquid to obtain solution 2 and residue 2, mixing solution 1 and solution 2, and adding FeS2After the reaction, carrying out solid-liquid separation to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates; adding ammonium bicarbonate into the solution 3, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate;|[0076] 3) recovering manganese waste residue from ferroalloy manganese dust by a wet method to extract manganese, a snow-melting agent and silicon dioxide micropowder, adding concentrated sulfuric acid into the residue 2 to react with water, and performing solid-liquid separation to obtain residue 3 and solution 4; b. reacting the residue 3 with 37% hydrochloric acid and water, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5 for reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain a snow-melting agent; c. adding 37% hydrochloric acid into the residue 4 to react with water, and performing solid-liquid separation to obtain residue 5 and solution 6; d, washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;|[0077] the solution 4 can be reused when the slag 1 is extracted by sulfuric acid; the washing waste water of solution 6 and residue 5 can be used for reacting residue 3 with 37% hydrochloric acid and water.|[0078] The methods of examples 1, 2 and 3 can be adopted in steps 1), 2) and 3), respectively.|[0079] The manganese content in the obtained manganese carbonate product is more than 43 percent; the content of manganese is increased, and the content of potassium oxide in the potassium sulfate is 40-50%; the silicon dioxide micro powder contains 85-95% of silicon oxide. (CN104313335)|TECHNICAL FIELD|[0002] The invention belongs to the technical field of metallurgy, and particularly relates to a wet separation and utilization method of ferroalloy manganese dust.|BACKGROUND ART|[0004] Manganese ore is an important basic bulk raw material mineral product for the industrial industry. Manganese is the most basic element of steel, and is an alloying element which has important influence on the performance of steel and steel products thereof, and all steel grades and steel products thereof contain manganese. Manganese is widely distributed in nature in many forms, and almost all kinds of ores and silicate rocks contain manganese minerals. The primary products of manganese ore comprise manganese ore for metallurgy, manganese carbonate mineral powder, manganese dioxide mineral powder for chemical industry, manganese oxide mineral powder for batteries and the like. The metallurgical industry is the largest of manganese ores|[0005] The main uses of the alloy are deoxidant and desulfurizer for iron making and steel making, and alloy manufacturing, more than 90% of the total output of manganese ore is used for producing manganese series ferroalloy in the world. China is a big country for producing manganese series ferroalloy and manganese metal, and the yield of the manganese series ferroalloy is more than 445 million tons. After the process for producing stainless steel by substituting nickel with manganese breaks through, the demand of electrolytic manganese metal is increased dramatically, and the yield of the electrolytic manganese metal is 60 ten thousand tons. The amount of the manganese ore used for metallurgy is more than 1000 ten thousand tons every year. Manganese accounts for about 3% of the total manganese used in the battery industry, and the amount of manganese used in the chemical industry (manganese dioxide ore powder is used as an oxidant and used for preparing manganese dioxide, manganese sulfate, potassium permanganate, manganese carbonate, manganese nitrate, manganese chloride and the like) accounts for about 2% of the total manganese; about 5% of manganese ore resources are used in other industries such as the light industry (matches, paints, soaps), the building material industry (colorants and discolorants for glass, ceramics and enamels), the electronics industry (magnetic materials), the environmental protection (adsorbents), the farming and animal husbandry (compound fertilizers, compound feeds) and the defense industry.|[0006] The worldwide-available and commercially-valuable manganese ore reserves are about 9-10 million tons, the global manganese metal distribution is obviously unbalanced, south africa and ukraine are two countries with the largest total amount of manganese ore resources in the world, the south africa manganese ore resources account for about 71.8 percent of the world manganese ore resources, and the ukraine accounts for 11.9 percent, wherein the four countries with the top-ranked world basic reserves account for 92.88 percent of the world total reserves.|[0007] The manganese resources in China are unbalanced in geographical distribution, the ore deposit is small in scale, the mining conditions are poor, the modern industrial technology is difficult to fully utilize for mining, more than 80% of the manganese ore yield comes from local small and medium mines and civil mines, and the yield is difficult to greatly improve. Meanwhile, the lean ores are more, the manganese-rich ores are less, the ore grade is low, the impurity content is high, the granularity is fine, the technical processability is poor, and the requirement of producing manganese series ferroalloy in China cannot be met. Moreover, the guarantee period of the existing manganese ore reserves is only 12 years.|[0008] At present, over ten countries abroad produce manganese ores, wherein the high-grade manganese ores are mainly produced in south Africa, Australia and galbanum, and the grade of manganese in the ores is generally 44-52%; the international manganese ore market is often in a state of short supply and short demand, basically is a seller market, and countries with rich manganese ore resources almost monopolize the pricing right of manganese ore.|[0009] Currently, the manganese-based alloy production in China is 745 million tons (excluding electrolytic manganese metal) as the largest manganese-based ferroalloy producing country in the world. The types of manganese ores in China are various, the material components are complex, the grade is low, the impurity content is high, the industrial application and the consumption field of the manganese ores with different types and impurities are greatly different or are respectively emphasized, so that millions of tons of high-quality manganese ores must be imported in China every year: firstly, the requirements of China on the production of high-grade manganese ferroalloy, particularly medium-low carbon ferromanganese are met; secondly, the imported ore is matched with domestic ore for use, so that domestic poor manganese oxide ore and poor manganese carbonate ore resources are reasonably and fully utilized, high ore price is integrated, and the raw material cost is reduced; thirdly, the index value of the technical requirement of the charging material is adjusted to achieve the purposes of strengthening smelting, increasing production and reducing consumption, improving the index and producing various grades of manganese alloys economically and reasonably.|[0010] The national development and reform committee "guide opinions on the comprehensive utilization of resources and notice of the comprehensive utilization embodiment of bulk solid waste" (issue modification ring fundamentals [2011] 2919) "defines" bulk industrial solid waste "as: the method refers to solid waste which is produced by more than 1,000 million tons in production activities in various industrial fields of China and has great influence on environment and safety, and mainly comprises the following steps: tailings, coal gangue, fly ash, smelting slag, industrial by-product gypsum, red mud and carbide slag.|[0011] The ferro-manganese dust of the ferro-manganese alloy is also called as smoke dust of ferromanganese smelting, is industrial powdery waste residue obtained by collecting dust generated by smoke dust generated in the process of producing the ferro-manganese alloy by high-temperature reduction with an electric furnace method, mainly contains elements such as iron, manganese, zinc, potassium and the like, and is a good secondary resource. However, because the Mn and Zn contents are low, the recycling of the manganese-iron alloy is difficult, the smoke dust and the fine manganese concentrate are mainly mixed and sintered in the industry at present and are returned to a production system for recycling, but the smoke dust loss of the method is large, and the normal furnace condition of the manganese-iron alloy smelting is influenced when the smoke dust is returned for use.|[0012] The ferroalloy manganese dust contains manganese 17-30%, potassium 5-20%, silicon dioxide 20-50%, carbon 1-5%, and also contains lithium, indium, gallium, germanium, zinc, lead, etc.|[0013] The manganese dedusting ash is manganese ore for metallurgy (YB/T319-2005) of a manganese mine according to the national ferrous metallurgy industry standard, and the manganese content of the manganese dedusting ash reaches B class and partially reaches A class.|[0014] The dedusting ash is used as sintering material to be put into the blast furnace again, but the sintering material brings great problems to the production of the blast furnace due to the rich alkali metals (potassium, sodium) and the like. The reuse causes the alkali metal to severely corrode equipment.|[0015] The literature, experimental research on leaching manganese from manganese dedusting ash (the Chinese manganese industry, 2 nd 2011), introduces the principle and process conditions of manganese series alloy smelting smoke dust wet leaching. Under certain technological conditions, pyrite is used as a reducing agent, manganese alloy smelting smoke dust with the Mn content of 28.95% is directly leached out by sulfuric acid, and the leaching rate reaches 93.22%.|[0016] In the document, manganese is extracted from manganese-based ferroalloy electric furnace environment-friendly fly ash containing complex manganese phases by a wet method, and more than 85% of manganese can be recovered.|[0017] In the experimental research on leaching of manganese and zinc from ferromanganese smelting smoke dust in the literature (the 5 th stage in 2014 of the chemical engineering progress), ferromanganese smelting smoke dust is used as a raw material, FeSO4.7H2O is used as a reducing agent, manganese and zinc elements enter a solution in the forms of Mn2+ and Zn2+ through sulfuric acid leaching, and the manganese and zinc elements are separated and extracted. Research shows that the optimal process conditions for leaching are as follows: the mass fraction of H2SO4 is 20%, the reaction time is 4H, the reaction temperature is 90 ℃, the liquid-solid ratio is 5: 1, the adding amount of reducing agent FeSO4.7H2O is 75g, and the stirring speed is 300 r/min. The leaching rate of manganese can reach 96.76 percent, and the leaching rate of zinc is 84.88 percent.|[0018] Traditionally, flotation equipment and flotation reagents (reducing agents) are adopted to select carbon, so that the environment and rear-end products are polluted.|[0019] The results of experiments on the potassium fertilizer application amount and the yield increase effect of rice in 10 provinces of China ever by the university of agriculture show that: according to the current fertilization standard, one kilogram of potash fertilizer is applied to each mu, and the yield of grains can be increased by 4-6 kilograms. Potash fertilizers also increase crop resistance to drought, frost and disease. According to data published by the national statistical bureau, the yield of summer grain in China is 2638 jin this year, and is increased by 39 jin compared with the yield in the last year, and the harvest of the summer grain is continuously realized in the 10 th year. This is greatly related to the amount of potash fertilizer in our country.|[0020] Data provided by the china association for inorganic salts show: nearly 700 million tons of potash fertilizer are imported from foreign countries every year in China. While the potassium minerals in the world are mainly in canada and russia, accounting for 46.3% and 34.7% of the world's total reserves, respectively. For transportation and tariff reasons, China mainly imports potash fertilizers from Russia. Among them, the Wular potash fertilizer company delivers about 250 ten thousand tons of potash fertilizer to China through railways and sea transportation every year.|[0021] The reserve of Chinese sylvite only accounts for 2.36% of the total reserve in the world, the reserve is mainly concentrated in the Qinghai Kao er salt lake and the Xinjiang Apocynum salt lake, and the mining quantities of the two mining areas are close to the limit. In 2010, the ministry of homeland resources determined that potassium salt is one of 8 bulk minerals in short supply in China.|[0022] At present, potassium ore resources are not only deficient in China, but also in agricultural countries such as the United states, Brazil, India and the like, and the competition for potassium ore resources in future is global.|DISCLOSURE|[0023] Disclosure of Invention|[0024] The invention aims to provide a wet separation and utilization method of ferroalloy manganese dust in order to fully utilize manganese dust, improve the value of the manganese dust and reduce the pollution to the environment.|[0025] The carbon removing and alkali metal reducing process of iron alloy manganese dust includes the following steps: mixing iron alloy manganese dust with water film dedusting wastewater, and reacting at 80-120 ℃; scraping carbon on the floating surface to obtain a carbon-removed material; the carbon scraped out is subjected to solid-liquid separation to obtain carbon powder;|[0026] the ratio of the iron alloy manganese dust to the water film dedusting wastewater is 1: 0.9-1.1; the reaction was carried out for 2 hours.|[0027] Method for extracting manganese and potassium fertilizer from iron alloy manganese dust|[0028] 1) Carrying out solid-liquid separation on the materials subjected to the decarbonization to obtain slag 1 and a solution 1;|[0029] 2) adding concentrated sulfuric acid and water into the slag 1, wherein the ratio of the slag to the concentrated sulfuric acid is 1: reacting at a water ratio of 1: 0.9-1.1; performing solid-liquid separation to obtain slag 2 and solution 2;|[0030] 3) mixing solution 1 and solution 2, and adding FeS at a molar ratio of 1-2: 42Carrying out solid-liquid separation after reaction at normal temperature to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates;|[0031] 4) adding ammonium bicarbonate into the solution 3, reacting at a molar ratio of 1: 0.9-1.1, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate;|[0032] the reaction in the step 2 is that the slag 1 reacts with concentrated sulfuric acid firstly, and then water is added for continuous reaction;|[0033] the concentration of the concentrated sulfuric acid is 90%;|[0034] step 4 the reaction time was 4 hours.|[0035] The method for extracting manganese, snow-melting agent and silicon dioxide micropowder from manganese waste residue recovered by ferroalloy manganese dust wet process comprises the following steps:|[0036] 1) adding concentrated sulfuric acid and water into the slag 2, and mixing the slag 2: concentrated sulfuric acid: reacting water = 1: 0.4-0.6: 1, and performing solid-liquid separation to obtain residue 3 and solution 4;|[0037] 2) adding 37% hydrochloric acid and water into residue 3, and mixing the following materials: acid: reacting water = 1: 0.35-0.45: 1, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5, reacting at a molar ratio of 1: 0.9-1.1, performing solid-liquid separation to obtain solid manganese carbonate, concentrating the liquid, and drying to obtain snow-melting agent;|[0038] 3) adding 37% hydrochloric acid and water into the residue 4, and mixing the materials according to the weight ratio of the residue 4: hydrochloric acid: reacting water = 1: 0.15-0.25: 1, and performing solid-liquid separation to obtain residue 5 and solution 6; .|[0039] 4) Washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;|[0040] the concentrated sulfuric acid is more than 70 percent.|[0041] The reaction in the step 1 is that the slag 2 reacts with concentrated sulfuric acid firstly, and then water is added for continuous reaction; the reaction in the step 2 is to react with hydrochloric acid firstly and then add water for continuous reaction.|[0042] The concentrated sulfuric acid is more than 90 percent.|[0043] The wet separating and utilizing process of iron alloy manganese dust includes the following steps:|[0044] 1) carbon removal and alkali metal reduction of iron alloy manganese dust: removing carbon from the ferroalloy manganese dust, and adding a reducing agent to perform a reduction reaction to obtain a material subjected to carbon removal;|[0045] 2) extracting manganese and potassium fertilizer from the ferroalloy manganese dust: performing solid-liquid separation on the decarbonized materials to obtain slag 1 and a solution 1; extracting residue 1 with sulfuric acid, separating solid and liquid to obtain solution 2 and residue 2, mixing solution 1 and solution 2, and adding FeS2After the reaction, carrying out solid-liquid separation to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates; adding ammonium bicarbonate into the solution 3, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate;|[0046] 3) recovering manganese waste residue from ferroalloy manganese dust by a wet method to extract manganese, a snow-melting agent and silicon dioxide micropowder, adding concentrated sulfuric acid into the residue 2 to react with water, and performing solid-liquid separation to obtain residue 3 and solution 4; b. reacting the residue 3 with 37% hydrochloric acid and water, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5 for reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain a snow-melting agent; c. adding 37% hydrochloric acid into the residue 4 to react with water, and performing solid-liquid separation to obtain residue 5 and solution 6; d, washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;|[0047] the solution 4 can be reused when the slag 1 is extracted by sulfuric acid; the washing waste water of solution 6 and residue 5 can be used for reacting residue 3 with 37% hydrochloric acid and water.|[0048] The method for removing carbon and reducing alkali metal from the iron alloy manganese dust, the method for extracting manganese and potash fertilizer from the iron alloy manganese dust, and the method for recovering manganese waste residue by using the wet method from the iron alloy manganese dust to extract manganese, a snow melting agent and silicon dioxide micropowder can be respectively adopted in the steps 1), 2) and 3).|[0049] The invention provides a wet separation and utilization method of ferroalloy manganese dust, which adopts water film dedusting wastewater as a reducing agent to remove carbon and reduce alkali metal from the ferroalloy manganese dust, and adopts sulfuric acid and FeS2Extracting to obtain manganese sulfate, adding ammonium bicarbonate to produce manganese carbonate and potassium sulfate (nitrogen-potassium fertilizer), and adding sulfuric acid and FeS2Washing the extracted residue with sulfuric acid, extracting with hydrochloric acid, adding ammonium bicarbonate into the extractive solution, reacting to obtain manganese carbonate, concentrating the solution to obtain snow-melting agent, washing the residue, pulverizing, and drying to obtain silica micropowder; the waste liquid in the production process is recycled; the manganese content in the obtained manganese carbonate product is more than 43 percent; improveManganese content, potassium oxide content in potassium sulfate 40-50%; the silicon dioxide micro powder contains 85-95% of silicon oxide. The iron alloy manganese dust is fully utilized; no reducing agent is added, water film dedusting wastewater is utilized, product quality is improved, output value is increased, and environment is protected.|[0050] The invention is characterized in that:|[0051] 1. the carbon in the fly ash is floated by steam (according to the special physical structure characteristics of the fly ash); compared with the traditional method of adopting flotation equipment and flotation reagent to select carbon, the method avoids reagent pollution on rear-end products, saves investment and production cost and obtains unexpected effects;|[0052] 2. the water film dedusting wastewater (absorbing reducing substances such as sulfite and the like generated by flue gas) is utilized to dissolve alkali metals (potassium and sodium) in the dedusting ash, and meanwhile, a foundation is laid for the reduction of high-valence manganese, and an unexpected effect is obtained;|[0053] 3. manganese carbonate, silicon dioxide micro powder, potassium sulfate compound fertilizer, environment-friendly snow-melting agent (calcium magnesium potassium chloride) and rare noble metal (nickel, cobalt, indium, gallium, germanium, zinc and lead) compounds are separated and extracted from the dust removal ash, and comprehensive utilization is realized in all directions without precedent.|[0054] 4. The technology of patent equipment authorized by independent intellectual property rights of the inventor is skillfully utilized, so that the process flow has the advantages of saving, reducing consumption, protecting environment, improving efficiency and the like in multiple directions.|DRAWINGS DESCRIPTION|[0056] FIG. 1 is a flow chart of the wet separation and utilization method of ferroalloy manganese dust.|INVENTION MODE|[0057] Detailed Description|INVENTION MODE|[0058] Example 1 method for removing carbon from iron alloy manganese dust and reducing alkali metal|[0059] The manganese-iron alloy is produced by high-temperature reduction in an electric furnace method, the generated smoke dust is collected by a cloth bag method; and the residual smoke dust is dedusted by a water film deduster, and water film dedusting wastewater is collected.|[0060] The solid-liquid ratio of the iron alloy manganese dust to the water film dedusting wastewater is 1: 1, mixing, introducing water vapor to ensure that the temperature of a reaction system is 80-120 ℃; a drum type reaction tank (ZL 200820072919.1) with a grinding device was used for 2 hours of reaction. Scraping carbon on the floating surface to obtain a carbon-removed material; and (3) carrying out solid-liquid separation on the scraped carbon by adopting an inorganic salt precipitate continuous washing machine (ZL 200920093696.1) to obtain carbon powder. This decarburizing process. Meanwhile, the water film dedusting wastewater (absorbing reducing substances such as sulfite generated by flue gas) is utilized to dissolve alkali metals (potassium and sodium) in the dedusting ash, and a foundation is laid for reducing high-valence manganese.|[0061] The ferro-alloy manganese dust is smoke dust generated in the process of producing ferro-manganese alloy by high-temperature reduction with an electric furnace method and collected by a dry method or a warm method.|[0062] The water film dedusting wastewater is the wastewater generated in the water film dedusting process in the process of producing ferromanganese alloy by high-temperature reduction with an electric furnace method|INVENTION MODE|[0063] Example 2 method for extracting manganese and potassium fertilizers from ferroalloy manganese dust|[0064] 1. Carrying out solid-liquid separation on the materials subjected to carbon removal in the embodiment 1 to obtain slag 1 and a solution 1;|[0065] 2. adding concentrated sulfuric acid and water into the slag 1, wherein the slag 1: concentrated sulfuric acid: the proportion of water is 1: 1: 1, the reaction was carried out using a drum type reaction tank (ZL 200820072919.1) equipped with a polishing apparatus. After 2 hours of reaction; performing solid-liquid separation to obtain slag 2 and solution 2;|[0066] 3. mixing solution 1 and solution 2, adding FeS2,FeS2Mixing with the mixed solution (molar ratio 1-2: 4) of solution 1 and solution 2, reacting at room temperature, and performing solid-liquid separation to obtain solution 3 and sulfide metal precipitate (nickel, cobalt, indium, gallium, zinc, and lead), which is formed by precipitation of sulfide metalAnd (4) concentrating wet separation.|[0067] 4. Adding ammonium bicarbonate (molar ratio 1: 1) into the solution 3 for reaction, after 4 hours of reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying potassium sulfate (nitrogen-containing potassium fertilizer) from the liquid.|INVENTION MODE|[0068] Example 3 method for extracting manganese, snow-melting agent and silica micropowder from manganese waste residue recovered from ferroalloy manganese dust by wet process.|[0069] 1. Adding concentrated sulfuric acid (material: concentrated sulfuric acid: water = 1: 0.5: 1) into the slag 2 for reaction, and carrying out solid-liquid separation to obtain slag 3 and a solution 4; the solution 4 can be returned to the slag 1 for utilization. The concentrated sulfuric acid concentration is more than 70%.|[0070] 2. Adding 37% hydrochloric acid (material: acid: water = 1: 0.4: 1) into the residue 3 for reaction, and carrying out solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5 for reaction (the molar ratio is 1: 1), after 4 hours of reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain a snow-melting agent (calcium magnesium potassium chloride composite salt);|[0071] 3. adding 37% hydrochloric acid (material: acid: water = 1: 0.2: 1) into the residue 4 for reaction, and performing solid-liquid separation to obtain residue 5 and solution 6; the solution 6 can be returned to the slag 3 for use.|[0072] 4. Washing the slag 5 with water (ZL 201120091074.2), separating solid and liquid, returning the solution 7 to the slag 3, washing the slag 5 with an inorganic salt precipitate continuous washing machine (ZL 200920093696.1), and crushing and drying the slag by a drying and crushing all-in-one machine (ZL 200920093766.3) to obtain the silicon dioxide micropowder.|[0073] The manganese content in the obtained manganese carbonate product is more than 43 percent; the manganese content in the manganese sulfate product produced by the existing method is more than 31 percent; the potassium oxide content in the potassium sulfate product is 40-50%; the silicon dioxide micro powder contains 85-95% of silicon oxide.|INVENTION MODE|[0074] Example 4 wet separation of ferroalloy manganese dust using method 1) decarbonization and alkali metal reduction of ferroalloy manganese dust: removing carbon from the ferroalloy manganese dust, and adding a reducing agent to perform a reduction reaction to obtain a material subjected to carbon removal;|[0075] 2) extracting manganese and potassium fertilizer from the ferroalloy manganese dust; carrying out solid-liquid separation on the decarbonized materials to obtain slag 1 and a solution 1; extracting residue 1 with sulfuric acid, separating solid and liquid to obtain solution 2 and residue 2, mixing solution 1 and solution 2, and adding FeS2After the reaction, carrying out solid-liquid separation to obtain a solution 3 and sulfide metal precipitates, and carrying out concentrated wet separation on the sulfide metal precipitates; adding ammonium bicarbonate into the solution 3, performing solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain potassium sulfate;|[0076] 3) recovering manganese waste residue from ferroalloy manganese dust by a wet method to extract manganese, a snow-melting agent and silicon dioxide micropowder, adding concentrated sulfuric acid into the residue 2 to react with water, and performing solid-liquid separation to obtain residue 3 and solution 4; b. reacting the residue 3 with 37% hydrochloric acid and water, and performing solid-liquid separation to obtain residue 4 and solution 5; adding ammonium bicarbonate into the solution 5 for reaction, carrying out solid-liquid separation to obtain solid manganese carbonate, and concentrating and drying the liquid to obtain a snow-melting agent; c. adding 37% hydrochloric acid into the residue 4 to react with water, and performing solid-liquid separation to obtain residue 5 and solution 6; d, washing the slag 5 with water, crushing and drying to obtain silicon dioxide micro powder;|[0077] the solution 4 can be reused when the slag 1 is extracted by sulfuric acid; the washing waste water of solution 6 and residue 5 can be used for reacting residue 3 with 37% hydrochloric acid and water.|[0078] The methods of examples 1, 2 and 3 can be adopted in steps 1), 2) and 3), respectively.|[0079] The manganese content in the obtained manganese carbonate product is more than 43 percent; the content of manganese is increased, and the content of potassium oxide in the potassium sulfate is 40-50%; the silicon dioxide micro powder contains 85-95% of silicon oxide. Family Number|(68525378)|68525378|Abstract|(CN104313335B B)|The invention discloses a wet separation utilization method of ferroalloy manganese dust . The method is as below : using water film dedusting wastewater as a reducing agent to conduct carbon removal and alkali metal reduction on ferroalloy manganese dust ; extracting by sulfuric acid and FeS2 to obtain manganese sulfate ; adding ammonium hydrogen carbonate to produce manganese carbonate and obtain potassium sulfate ( potash fertilizer nitrogen ) ; washing the residue from sulfuric acid and FeS2 extraction ; extracting with hydrochloric acid ; adding ammonium hydrogen carbonate into the extracting solution for reaction to obtain manganese carbonate ; concentrating the solution to obtain a snow melting agent ; washing , crushing and drying the residue to obtain fine silica powder ; and reusing the waste liquid in the production process . The prepared manganese carbonate product has manganese content greater than 43% to increase the Mn content ; the potassium oxide content in potassium sulfate is 40-50% ; and silicon oxide content in silica powder is 85-95%. The method fully uses ferroalloy manganese dust , does not need the addition of reducing agent , uses the water film dedusting wastewater , improves product quality , increases output , and protects the environment . |IPC codes|(CN104313335B B)|C01B - 032/60 |C01B - 033/12 |C01D - 005/06 |C01G - 045/00 | Basic materials chemistry|Materials, metallurgy Y02W-030/50 Y02W-030/50 C01B-032/60|C01B-033/12|C01D-005/06|C01G-045/00|C09K-003/18|C21B-003/04|C22B-005/10|C22B-007/02|C22B-026/10|C22B-047/00 C01B-031/24|C01B-033/12|C01D-005/06|C01G-045/00|C09K-003/18|C21B-003/04|C22B-005/10|C22B-007/02|C22B-026/10|C22B-047/00 CN117660768|CN114524460|CN105905925|CN106636653B CN117660768 108767924 WHO=Examiner SELF=N CAT=A|CN114524460 100169037 WHO=Examiner SELF=N CAT=A|CN105905925 74052028 WHO=Examiner SELF=N CAT=A|CN106636653B 76087288 WHO=Examiner SELF=N CN1382813|JP5229416 CN1382813 4953288 WHO=Examiner SELF=N CAT=X|JP5229416 44688928 WHO=Examiner SELF=N CAT=A 唐华应等: &quot;从锰除尘灰中湿法回收锰&quot;, 《湿法冶金》 (Cat. A)|谢红艳等: &quot;从锰除尘灰中浸出锰的实验研究&quot;, 《中国锰业》 (Cat. A) CN1382813; JP5229416 LAPSED (CN104313335)|LAPSED DEAD (CN104313335)|DEAD (CN104313335)|LEGAL DETAILS FOR CN104313335|Actual or expected expiration date=2018-09-23|Legal state=DEAD|Status=LAPSED|Event publication date=2014-09-23|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201410486205|Application date=2014-09-23|Standardized application number=2014CN-0486205|Event publication date=2015-01-28|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN104313335|Publication stage code=A|Publication date=2015-01-28|Standardized publication number=CN104313335|Event publication date=2015-01-28|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2015-02-25|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2016-09-14|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN104313335|Publication stage code=B|Publication date=2016-09-14|Standardized publication number=CN104313335B|Event publication date=2016-09-14|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2016-09-14|Event code=CN/TA01|Event group=Change of name or address Reassignment|Transfer of the patent application right or the patent right|FORMER APPLICANT:Jilin City Friend Technology Co., Ltd. FORMER APPLICANT:JILIN FRIEND TECHNOLOGY CO. LTD. APPLICANT:Zheng Jingyi APPLICANT:ZHENG JINGYI|Effective date of the event=2016-08-23|Event publication date=2019-09-10|Event code=CN/CF01|Event indicator=Neg|Event group=Event indicating Not In Force|Termination of patent right due to non-payment of annual fee|Effective date of the event=2018-09-23 https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjkfSZC7jo+s5Bj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000013830845&ekey=2278&xpn=CN104313335B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=7ytTyTt8sUqc4IjO1x2P3bmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN104313335)|CN (CN104313335)|NAME=ZHENG JINGYI , COUNTRY=CN (CN104313335)|NAME=ZHANG TIESHENG;CHANGCHUN DONGSHI PATENT LAW OFFICE , REG=22202|(CN104313335)|NAME=ZHANG TIESHENG;CHANGCHUN DONGSHI PATENT LAW OFFICE (CN104313335)|NAME=ZHENG JINGYI|NAME=LÜ WENGUANG|(CN104313335)|NAME=ZHENG JINGYI|NAME=LÜ WENGUANG 0 1 Titre: (CN104313335)|Wet separation and utilization method of ferroalloy manganese dust Résumé: (CN104313335)|The invention discloses a wet separation utilization method of ferroalloy manganese dust. The method is as below: using water film dedusting wastewater as a reducing agent to conduct carbon removal and alkali metal reduction on ferroalloy manganese dust; extracting by sulfuric acid and FeS2 to obtain manganese sulfate; adding ammonium hydrogen carbonate to produce manganese carbonate and obtain potassium sulfate (potash fertilizer nitrogen); washing the residue from sulfuric acid and FeS2 extraction; extracting with hydrochloric acid; adding ammonium hydrogen carbonate into the extracting solution for reaction to obtain manganese carbonate; concentrating the solution to obtain a snow melting agent; washing, crushing and drying the residue to obtain fine silica powder; and reusing the waste liquid in the production process. The prepared manganese carbonate product has manganese content greater than 43% to increase the Mn content; the potassium oxide content in potassium sulfate is 40-50%; and silicon oxide content in silica powder is 85-95%. The method fully uses ferroalloy manganese dust, does not need the addition of reducing agent, uses the water film dedusting wastewater, improves product quality, increases output, and protects the environment. 91 Abstract gpt-4o-mini no The article focuses on a method for processing ferroalloy manganese dust and does not mention accelerated weathering, CO₂ capture, or related mineral carbonation processes.
93 CN201310380093 CN201310380093 CN103483019 59506227 CN103483019 A 2014-01-01 [CN103483019] 2013-08-28 2013-08-28 2014-01-01 (CN103483019)|2019-08-23 (CN103483019)|Biological active fertilizer taking branch and fallen leaf of poplar as raw materials and application method thereof (CN103483019)|The invention discloses a biological active fertilizer taking the branches and fallen leaves of poplar as raw materials and an application method thereof. The effective component of the biological active fertilizer takes the branches and fallen leaf crushed substances of the poplar and vermiculite as main raw materials. The preparation method comprises the following steps of: mixing the branches and fallen leaf crushed substances of the poplar and the vermiculite according to the volume ratio of 2:1, and then mixing into MMN liquid culture medium; inoculating multiple ectomycorrhizal fungus, and then uniformly mixing with biological active carbon, a biological organic fertilizer, a water retention agent and a biological active growth-promoting component under an aseptic condition to obtain a solid biological mycorrhiza formulation. Compared with the traditional biological fertilizer, the biological active fertilizer disclosed by the invention can obviously enhance the absorption of multiple nutrient elements of a plant root system, promote the growth of a seedling, enhance the tolerance and soil-borne diseases and insect pests resistant capacity of a plant on a drought environment, a saline-alkali environment, an impoverished environment, and the like, activate the beneficial microbes contained in rhizosphere soil, enhance the photosynthesis, enhance the carbon sequestration capacity of the plant, optimize the seedling quality and increase the market value. ZHOU JINXING (CN103483019)|ZHOU JINXING CUI MING|ZHOU JINXING|YU MENG|QIN YONGSHENG|WANG XIAOPING|LIU YUGUO (CN103483019)|CUI MING|ZHOU JINXING|YU MENG|QIN YONGSHENG|WANG XIAOPING|LIU YUGUO (CN103483019)|Compared with the prior art, the invention has the advantages that: the bioactive fertilizer produced by the invention can be widely applied to landscaping engineering of various commonly used afforestation tree species such as coniferae, fagaceae, salicaceae, betulinaceae and the like in northern areas of China, can obviously improve the absorption of plant roots to water and various nutrient elements such as nitrogen, phosphorus, potassium, calcium, magnesium, sulfur, iron, manganese, copper, zinc, nickel and the like, promotes the growth of seedlings, can improve the tolerance of plants to environments such as drought, saline-alkali and infertile and the capability of resisting soil-borne diseases and insect pests, and reduces the use of pesticides; activating beneficial microorganisms in rhizosphere soil; enhancing photosynthesis and improving carbon fixation capacity of plants; the quality of the nursery stock is optimized, and the market value is increased.|Foreign bacterial manure technology is mature and has been popularized and applied in many fields, however, foreign soil conditions and common greening tree species are greatly different from those in China, and foreign bacterial manure is not always effective for the common greening tree species in China, such as Chinese pine, and is unknown whether to cause environmental problems such as ecological invasion.| (CN103483019)|1. A biological active fertilizer taking poplar branches and fallen leaves as raw materials and an application method thereof are characterized in that: the effective components of the composite are mainly prepared from poplar branches and fallen leaves crushed materials and vermiculite, wherein the volume ratio of the poplar branches and fallen leaves crushed materials to the vermiculite is 2: 1, mixing, then mixing with an MMN liquid culture medium, culturing at a constant temperature of 25 ℃ for 15 days, inoculating various ectomycorrhizal fungi, when hyphae grow over the culture bag for standby, uniformly mixing with biological activated carbon, a biological organic fertilizer, a water-retaining agent and a biological activity promoting component under an aseptic condition, wherein the biological activated carbon accounts for 15% of the total volume of the biological mycorrhizal preparation, the biological organic fertilizer accounts for 25% of the total volume of the biological mycorrhizal preparation, the addition amount of the water-retaining agent is 5% of the total volume of the biological mycorrhizal preparation, and the biological activity promoting component accounts for 1% of the total volume of the biological mycorrhizal preparation, so that the solid biological myco.| (CN103483019)|In order to achieve the purpose, the invention adopts the technical scheme that: a biological active fertilizer taking poplar branches and fallen leaves as raw materials and an application method thereof are disclosed, wherein the active ingredients of the fertilizer take crushed poplar branches and fallen leaves and vermiculite as main raw materials, and the crushed poplar branches and fallen leaves and the vermiculite are mixed according to the volume ratio of 2: 1, mixing, then mixing with an MMN liquid culture medium, culturing at a constant temperature of 25 ℃ for 15 days, inoculating various ectomycorrhizal fungi, when hyphae grow over the culture bag for standby, uniformly mixing with biological activated carbon, a biological organic fertilizer, a water-retaining agent and a biological activity promoting component under an aseptic condition, wherein the biological activated carbon accounts for 15% of the total volume of the biological mycorrhizal preparation, the biological organic fertilizer accounts for 25% of the total volume of the biological mycorrhizal preparation, the addition amount of the water-retaining agent is 5% of the total volume of the biological mycorrhizal preparation, and the biological activity promoting component accounts for 1% of the total volume of the biological mycorrhizal preparation, so that the solid biological myco.|The invention discloses a biological active fertilizer taking poplar branches and fallen leaves as raw materials and an application method thereof, wherein the active ingredients of the biological active fertilizer take crushed poplar branches and fallen leaves and vermiculite as main raw materials, and the crushed poplar branches and fallen leaves and the vermiculite are mixed according to the volume ratio of 2: 1, mixing, then mixing with an MMN liquid culture medium, inoculating a plurality of ectomycorrhizal fungi, and then uniformly mixing with biological activated carbon, a biological organic fertilizer, a water-retaining agent and a biological activity growth promoting component under a sterile condition to obtain the solid biological mycorrhizal preparation.|The invention relates to an active fertilizer and an application method thereof, in particular to a biological active fertilizer taking branches and fallen leaves of poplar as raw materials and an application method thereof.| (CN103483019)|FALLEN LEAVE(100,17)|RAW MATERIAL(100,12)|POPLAR BRANCH(100,9)|BIOACTIVE FERTILIZER(100,7)|FERTILIZER ACTIVITY(100,7)|CRUSHED POPLAR BRANCH(100,5)|FOREIGN BACTERIAL MANURE(68,2)|MYCORRHIZAL TOTAL VOLUME(65,8)|VERMICULITE(44,8)|ENHANCING PHOTOSYNTHESIS(42,2)|SOLID BIOLOGICAL MYCO(41,2)|NURSERY STOCK(39,10)|RHIZOSPHERE SOIL(37,3)|ECTOMYCORRHIZAL FUNGUS(36,5)|STERILE CONDITION(36,3)|ECOLOGICAL INVASION(36,1)|ACTIVE FERTILIZER ACTIVE INGREDIENT(33,1)|SOLID MYCORRHIZAL(33,1)|CULTURE BAG(32,4)|POPLAR FALLEN LEAVE(32,4)|FERTILIZER ACTIVE INGREDIENT(32,1)|ACTIVE INGREDIENT(31,2)|CHINESE PINE(31,1)|TOTAL VOLUME(30,8)|ORGANIC FERTILIZER ACCOUNT(29,2)|MMN LIQUID CULTURE MEDIUM(28,4)|FALLEN LEAVE CRUSHED MATERIAL(27,2)|BIOLOGICAL ACTIVITY(25,4)|NURSERY STOCK GROWTH(25,2)|ORGANIC FERTILIZER(24,4)|AFFORESTATION TREE SPECIES(23,2)|PLANT CARBON FIXATION CAPACITY(23,2)|TRANSPLANTING SEEDLING(23,2)|MICROORGANISM(22,3)|FOREIGN LAND CONDITION(22,1)|SOLID MICROBIAL INOCULUM FERTILIZER(21,3)|COMPONENT ACCOUNT(21,2)|STANDBY(21,2)|ANNULAR DITCH(20,6)|SOIL BORNE DISEASE(20,2)|ACTIVATED CARBON ACCOUNT(19,2)|POPLAR BRANCH VOLUME RATIO(19,1)|WATER RETAINING(18,5)|CARBON FIXATION CAPACITY(18,2)|ACTIVATED CARBON(17,3)|EXPOSING ABSORBED ROOT(17,3)|BIOLOGICAL ACTIVITY GROWTH(17,2)|LIQUID CULTURE MEDIUM(16,5)|DROUGHT(16,3)|INSECT PEST(16,3)|CRUSHED MATERIAL(16,2)|NUTRIENT(16,2)|SOIL BORNE PLANT DISEASE(16,1)|MATRIX SOIL(14,3)|TREE SPECIES(14,3)|CONSTANT TEMPERATURE(13,2)|CARBON FIXATION(12,2)|PESTICIDE(12,2)|NORTHERN AREA(12,1)|TREE TRUNK(11,5)|IRRIGATION LIQUID(11,3)|MANGANESE(11,2)|PHOSPHORUS(11,2)|PLANT ROOT(9,9)|MYCORRHIZA FERTILIZER(9,3)|SULFUR(9,2)|VOLUME RATIO(8,5)|WATERING(8,3)|FORESTRY REALIZING SUSTAINABLE DEVELOPMENT(8,2)|MYCORRHIZAL BIOFERTILIZER(8,2)|PT MYCORRHIZAL INOCULANT(8,1)|AUTUMN(7,3)|EDEN PLANT SEEDLING CULTURE(7,1)|MARKET VALUE(6,3)|GARBAGE MOUNTAIN(6,2)|ENDOPHYTIC MYCORRHIZAL FUNGUS(6,1)|MYCORRHIZA ABSORPTION ORGAN(6,1)|ULTRACLEAN WORKBENCH(6,1)|ENVIRONMENT POLLUTION(5,2)|POLLUTANT STRESS(5,2)|BOLETE PACHYCHNO(5,1)|BOLETUS RUDUCEN(5,1)|BOLETUS RUGOSUS(5,1)|CERCOSPORA ERYTHRAEA(5,1)|CULTURED MYCORRHIZAL FUNGUS(5,1)|EXOGENOUS MYCORRHIZAL FUNGUS(5,1)|MYCORRHIZAL FERTILIZER(5,1)|PLANT SUCCESSTM TAB(5,1)|POLLUTANT TRANSPORTATION(5,1)|AFFORESTATION SURVIVAL RATE(4,3)|COTTON PLUG(4,2)|FIELD PLANTING(4,2)|AGRICULTURE REQUIREMENT(4,1)|BOLETE EDULIS(4,1)|BOLETE FUSCA(4,1)|CRUSHED BRANCH(4,1)|CRUSHED POPLAR(4,1)|CRUSHING(4,1)|ECOLOGICAL SIGNIFICANCE(4,1)|EXTRACELLULAR GLYCOPROTEIN(4,1)|FOREST TREE(4,1)|GREENING TREE(4,1)|HUGE MYCELIUM(4,1)|KNOT NEMATODE(4,1)|LACCA LACCATA(4,1)|MYCORRHIZA CREATION(4,1)|MYCORRHIZA RESEARCH(4,1)|PERMANENT WITHERING(4,1)|PLANT TOXICITY(4,1)|POLLUTANT DEGRADATION(4,1)|POLYETHYLENE CULTURE BAG(4,1)|SCREENED VERMICULITE(4,1)|SIEVING VERMICULITE(4,1)|SOIL BORNE PATHOGENIC FUNGUS(4,1)|TRANSPLANTING PLANT(4,1)|COMETABOLISM(3,2)|DAMAGING ENVIRONMENT(3,2)|MASS MILL(3,2)|SILICA PLUG(3,2)|COOL MORNING(3,1)|ECOLOGICAL PROTECTION(3,1)|ENVIRONMENT FRIENDLY AGRICULTURE(3,1)|GERMAN PLANT PATHOLOGIST(3,1)|GROWTH PROMOTION(3,1)|HUGE REQUIREMENT(3,1)|HYPHA NETWORK(3,1)|MMN LIQUID CULTURE LITER(3,1)|MYCORRHIZA FORMATION(3,1)|PINE GROWTH(3,1)|PLANT INSECT PEST(3,1)|ROOT ABSORPTION(3,1)|TISSUE FUNGUS(3,1)|UNUSED PLANT(3,1)|CONVERSION CAPACITY(2,2)|USED AFFORESTATION TREE SPECIES(2,2)|BACTERIA(2,1)|BARREN RESISTANCE(2,1)|CARBON RESERVE(2,1)|CORE IDEA(2,1)|FARMING CONDITION(2,1)|FINE CRACK(2,1)|FOREST COST(2,1)|GOMPHIDIUS ROSEUS(2,1)|GROUND STABILITY(2,1)|MYCORRHIZA INFECTION RATE(2,1)|MYCORRHIZA SURVIVAL RATE(2,1)|MYCORRHIZAL FUNGUS AGENT PRODUCTION(2,1)|PHOTOSYNTHESIS(2,1)|PLANT ALKALINE RESISTANCE(2,1)|PLANT CARBON SEQUESTRATION CAPACITY(2,1)|POLLUTION FREE BIOLOGICAL FERTILIZER(2,1)|POPULARIZATION(2,1)|PRODUCING ANIMAL HUSBANDRY(2,1)|ROOT GROWTH(2,1)|SOIL ENVIRONMENT(2,1)|STERILE ENVIRONMENT(2,1)| (CN103483019)|1. A biological active fertilizer taking poplar branches and fallen leaves as raw materials and an application method thereof are characterized in that: the effective components of the composite are mainly prepared from poplar branches and fallen leaves crushed materials and vermiculite, wherein the volume ratio of the poplar branches and fallen leaves crushed materials to the vermiculite is 2: 1, mixing, then mixing with an MMN liquid culture medium, culturing at a constant temperature of 25 ℃ for 15 days, inoculating various ectomycorrhizal fungi, when hyphae grow over the culture bag for standby, uniformly mixing with biological activated carbon, a biological organic fertilizer, a water-retaining agent and a biological activity promoting component under an aseptic condition, wherein the biological activated carbon accounts for 15% of the total volume of the biological mycorrhizal preparation, the biological organic fertilizer accounts for 25% of the total volume of the biological mycorrhizal preparation, the addition amount of the water-retaining agent is 5% of the total volume of the biological mycorrhizal preparation, and the biological activity promoting component accounts for 1% of the total volume of the biological mycorrhizal preparation, so that the solid biological myco.|2. The bioactive fertilizer taking poplar branches and fallen leaves as raw materials and the application method thereof according to claim 1 are characterized in that: there are three methods of application that are described,|the direct application method comprises the following steps: during seedling transplanting and field planting, annular ditches are dug around root systems, the depth is proper for exposing absorbed roots, microbial inoculum fertilizer is scattered into the ditches and is uniformly mixed with soil, the microbial inoculum fertilizer is contacted with the root systems as much as possible, then soil is covered, watering is carried out, and the using amount is calculated by applying 150g of the fertilizer per 2.5 centimeters of the diameter of a tree trunk;|secondly, a liquid irrigation method: when the nursery stock is transplanted and planted, annular ditches are dug around the root system, the depth is suitable for exposing and absorbing roots, solid microbial inoculum fertilizer is diluted by 30-40 times by adding water, 30-40kg of water is added into 1kg of microbial inoculum, the mixture is uniformly stirred and poured into soil, and the using amount is calculated by applying 1 liter of water according to the diameter of each 2.5 cm of the tree trunk;|③ matrix soil method: when the seedlings are transplanted and planted, the seedlings are applied according to the size of a container by 3 g/L, and the best application is spring and autumn. (CN103483019)|TECHNICAL FIELD|[0002] The invention relates to an active fertilizer and an application method thereof, in particular to a biological active fertilizer taking branches and fallen leaves of poplar as raw materials and an application method thereof.|BACKGROUND ART|[0004] The mycorrhiza fertilizer is a novel efficient, nontoxic, green and pollution-free biological fertilizer, can meet the requirements of agriculture and forestry product production and ecological protection, and has wide market prospect.|[0005] Mycorrhiza research has been on for over 100 years since the creation of mycorrhiza by Frank, a german plant pathologist in 1885. The mycorrhizal fungi have huge hypha systems and are tightly connected with plant root systems into a whole to form mycorrhiza, are the most widely distributed and important symbionts in the biological world, and have important significance for promoting the exchange and transmission of substances, energy and information among organisms in various ecological systems. Meanwhile, the method has profound economic, social and ecological significance for keeping ecological balance and sustainable development, protecting biological diversity, stabilizing an ecological system and promoting agriculture, forestry and animal husbandry production.|[0006] The huge mycelium spread in the soil is a main absorption organ of mycorrhiza, after the plant forms the mycorrhiza, the density of the absorbed root is increased, the root form is changed, the mycelium can go deep into soil and rock fine cracks which cannot be reached by the original plant root system, the absorption range of water and nutrients of the plant is expanded to a great extent, and therefore the biomass of the plant is improved. The mycorrhizal fungi can also activate mineral elements in soil and promote the absorption of nutrient elements by plant roots, especially the absorption of phosphorus with poor mobility and mineral elements such as zinc, copper and the like. The formation of mycorrhiza can reduce the permanent withering point of the plant and improve the drought resistance and the water utilization efficiency of the plant. In addition, the mycorrhizal fungi are inoculated to the plants, the resistance of the plants in the adverse environment can be enhanced, the survival rate of the plants is improved, the barren resistance, cold resistance and saline and alkaline resistance of the plants are enhanced, and after the mycorrhizal fungi and the root systems of the plants form mycorrhiza, the plant diseases, especially plant insect pests such as soil-borne pathogenic fungi, cyst nematodes, root knot nematodes and the like can be greatly reduced. Extracellular glycoprotein secreted by mycorrhiza is combined with hypha network, which is beneficial to the formation of soil aggregate structure, can improve soil stability, maintain soil porosity, ensure good farming condition and ventilation condition, fix organic matters in soil and improve carbon reserve in soil. The mycorrhiza can also reduce the pollution to the soil environment and the adverse effect to plants caused by heavy metal, organic pollutant, radioactive elements and the like, plants using the mycorrhiza fertilizer can absorb more heavy metal and organic pollutant than unused plants without toxicity, the organic acid secreted by the mycorrhiza fertilizer can complex the pollutant, thereby reducing the toxicity of the plant, simultaneously reducing the transportation of the pollutant from the root to the overground part, being an important storage warehouse for fixing the pollutant in the soil and having great value in pollutant degradation.|[0007] At present, the mycorrhizal fungi agents are produced by companies in many countries and are widely applied, such as the United states, Europe, Japan, Taiwan and the like. The method is mainly used for transplanting plants, such as flowers, fruit trees, greening trees and the like.|[0008] A mycorrhizal fungi agent- -rootgrowth (TM) for arid areas is researched and developed in East of Eden Plants seedling culture center in England, the fungi agent contains at least 5 mycorrhizal fungi, and can adapt to water stress, and the survival rate of seedlings can be improved by inoculating the fungi agent. The tissue Fungi PerfectR authorized in Washington, USA also has a plurality of mycorrhizal Fungi agent products, wherein the Plant SuccessTM Tabs contain 12 kinds of endophytic and exogenous mycorrhizal Fungi, and the Fungi agent can promote the growth of plants and root systems, improve the absorption of nutrients and water and reduce the use of fertilizers.|[0009] Although most mycorrhizal fungi can infect various tree species and can adapt to complex environmental conditions, the effect of achieving twice the result with half the effort can be achieved only by following the principle of being suitable for trees as much as possible in the using process. Foreign bacterial manure technology is mature and has been popularized and applied in many fields, however, foreign soil conditions and common greening tree species are greatly different from those in China, and foreign bacterial manure is not always effective for the common greening tree species in China, such as Chinese pine, and is unknown whether to cause environmental problems such as ecological invasion. In addition, the price is high, and the popularization in the garden greening of China is difficult.|[0010] The Pt mycorrhizal inoculant developed by China forestry science research institute, namely the Jianbao, has single species, the effective bacteria are mainly puffball species, the application range is narrow, and the huge requirements of the current landscaping can not be met.|DISCLOSURE|[0011] Disclosure of Invention|[0012] The invention aims to solve the problems, and the invention provides the bioactive fertilizer which takes poplar branches and fallen leaves as raw materials, can effectively promote the growth of pine and oak trees, has simple and convenient use method and low cost, obviously improves the activity of plant root systems after being used, improves soil, enhances the disease resistance and stress resistance of plants, and improves the survival rate of mycorrhiza and the application method thereof.|[0013] In order to achieve the purpose, the invention adopts the technical scheme that: a biological active fertilizer taking poplar branches and fallen leaves as raw materials and an application method thereof are disclosed, wherein the active ingredients of the fertilizer take crushed poplar branches and fallen leaves and vermiculite as main raw materials, and the crushed poplar branches and fallen leaves and the vermiculite are mixed according to the volume ratio of 2: 1, mixing, then mixing with an MMN liquid culture medium, culturing at a constant temperature of 25 ℃ for 15 days, inoculating various ectomycorrhizal fungi, when hyphae grow over the culture bag for standby, uniformly mixing with biological activated carbon, a biological organic fertilizer, a water-retaining agent and a biological activity promoting component under an aseptic condition, wherein the biological activated carbon accounts for 15% of the total volume of the biological mycorrhizal preparation, the biological organic fertilizer accounts for 25% of the total volume of the biological mycorrhizal preparation, the addition amount of the water-retaining agent is 5% of the total volume of the biological mycorrhizal preparation, and the biological activity promoting component accounts for 1% of the total volume of the biological mycorrhizal preparation, so that the solid biological myco.|[0014] Preferably, there are three methods of administration,|[0015] the direct application method comprises the following steps: during seedling transplanting and field planting, annular ditches are dug around root systems, the depth is proper for exposing absorbed roots, microbial inoculum fertilizer is scattered into the ditches and is uniformly mixed with soil, the microbial inoculum fertilizer is contacted with the root systems as much as possible, then soil is covered, watering is carried out, and the using amount is calculated by applying 150g of the fertilizer per 2.5 centimeters of the diameter of a tree trunk;|[0016] secondly, a liquid irrigation method: when the nursery stock is transplanted and planted, annular ditches are dug around the root system, the depth is suitable for exposing and absorbing roots, solid microbial inoculum fertilizer is diluted by 30-40 times by adding water, 30-40kg of water is added into 1kg of microbial inoculum, the mixture is uniformly stirred and poured into soil, and the using amount is calculated by applying 1 liter of water according to the diameter of each 2.5 cm of the tree trunk;|[0017] ③ matrix soil method: when the seedlings are transplanted and planted, the seedlings are applied according to the size of a container by 3 g/L, and the best application is spring and autumn.|[0018] Compared with the prior art, the invention has the advantages that: the bioactive fertilizer produced by the invention can be widely applied to landscaping engineering of various commonly used afforestation tree species such as coniferae, fagaceae, salicaceae, betulinaceae and the like in northern areas of China, can obviously improve the absorption of plant roots to water and various nutrient elements such as nitrogen, phosphorus, potassium, calcium, magnesium, sulfur, iron, manganese, copper, zinc, nickel and the like, promotes the growth of seedlings, can improve the tolerance of plants to environments such as drought, saline-alkali and infertile and the capability of resisting soil-borne diseases and insect pests, and reduces the use of pesticides; activating beneficial microorganisms in rhizosphere soil; enhancing photosynthesis and improving carbon fixation capacity of plants; the quality of the nursery stock is optimized, and the market value is increased. In addition, after the mycorrhizal fungi and the plants are formed together, the degradation and conversion capacity of pollutants can be improved through the co-metabolism, the stress of the pollutants in mining area waste land, petroleum, heavy metal polluted soil, garbage mountain and other areas to trees is relieved, the afforestation survival rate is improved, and the polluted and damaged environment is repaired. The application of the mycorrhizal biofertilizer is a development direction of green industry in the future and is also one of effective ways for realizing sustainable development of forestry.|INVENTION MODE|[0019] Detailed Description|[0020] The present invention will be further explained below,|[0021] example (b): a bioactive fertilizer using branches and fallen leaves of poplar as raw materials and its application method are disclosed, which comprises the following steps, using the crushed branches and fallen leaves of poplar and vermiculite as main raw materials,|[0022] sieving vermiculite, and taking a part with the particle size larger than 1mm for later use;|[0023] crushing branches and fallen leaves of the poplar, and sieving to obtain parts with the grain size of 1-10 mm for later use;|[0024] thirdly, putting the screened vermiculite and the crushed poplar branches into an autoclave respectively for sterilization treatment, cooking for 2 hours at 121 ℃, spreading the materials after cooking, and cooling;|[0025] fourthly, mixing the crushed poplar branches and vermiculite according to a volume ratio of 2: 1, and mixing the mixture with an MMN liquid culture medium, wherein the mass ratio of the materials to the liquid culture medium is 1: 1.2-1.5, and after uniformly stirring, tightly holding by hand to allow liquid to seep out, wherein each liter of MMN liquid culture medium comprises the following components: CaCl20.05g;MgSO4 0.15g;NaCl 0.025g;FeCl3 (1%)1.2ml;KH2PO40.5 g; VitamibB1 (thiamine) 100 μ g; (NH)4)2HPO40.25 g; peptone (12 Be') 100 ml; 10-15g of Glucose; 0.2g of citric acid; 900ml of distilled water; pH5.5 or so;|[0026] fifthly, filling the mixed materials into a polyethylene culture bag (17 x 33cm), plugging a cotton plug or a silica gel plug, tying the cotton plug or the silica gel plug by a rubber band, and sterilizing the mixture for 30min at the temperature of 121 ℃;|[0027] sixthly, after the culture bags (17 x 33cm) filled with the materials are cooled to room temperature, inoculating various ectomycorrhizal fungi in an ultra-clean workbench or a sterile room or a sterile environment, wherein the inoculation amount of each bag is 5-10%, and the various ectomycorrhizal fungi are inoculated into bolete pachychnos (Suillus grevillei), bolete fusca (Suillusluteus), bolete edulis (Boletus edulis), Boletus ruducens (Xerocomuschrysenton), Boletus rugosus (Gomphidius roseus) and cercospora erythraea (Lacca laccata);|[0028] seventhly, culturing in a greenhouse or an incubator at 25 ℃ in a dark place, and growing the whole bag after 15 days;|[0029] the cultured mycorrhizal fungi which are taken as main bioactive substances are mixed with the biological active carbon and the organic fertilizer according to the volume ratio of 12: 3: 5, uniformly mixing, adding the biological water-retaining agent according to 5 per mill of the mass of the mixture, adding the biological activity growth promoting component according to 1 per mill of the mass of the mixture, and uniformly mixing to prepare the microbial inoculum fertilizer;|[0030] ninthly, after being packaged, the product is stored in a shady and cool place or a refrigerator at 4 ℃.|[0031] There are three methods of application of the present invention,|[0032] the direct application method comprises the following steps: when the nursery stock is transplanted and planted, annular ditches are dug around the root system to a depth suitable for exposing absorbed roots, microbial inoculum fertilizer is scattered into the ditches and is uniformly mixed with soil, the fertilizer is contacted with the root system as much as possible, then soil is covered, and watering is carried out, wherein the using amount is calculated by applying 150g per 2.5 cm of the diameter of the trunk.|[0033] Secondly, a liquid irrigation method: when the nursery stock is transplanted and planted, annular ditches are dug around the root system, the depth is suitable for exposing and absorbing roots, solid microbial inoculum fertilizer is diluted by 30-40 times by adding water, 30-40kg of water is added into 1kg of microbial inoculum, the mixture is uniformly stirred and poured into soil, and the using amount is calculated by applying 1 liter of water according to the diameter of each 2.5 cm of the tree trunk.|[0034] ③ matrix soil method: when the nursery stock is transplanted and planted, the microbial inoculum fertilizer is applied according to the size of a container by 3 g/L, for example, 15g is added into a 5L flowerpot, and the best is spring and autumn when the microbial inoculum is applied. In summer, the cool morning or evening should be selected to avoid the high temperature weather.|[0035] After application, mycorrhiza can be formed in 2-3 months generally, the infection rate of the mycorrhiza can reach more than 80%, and the growth promoting effect is obvious after 1 year.|[0036] The biological active fertilizer produced by the invention can be widely applied to landscaping engineering of various commonly used afforestation tree species in northern China, such as coniferae, fagaceae, salicaceae, betulinaceae and the like. After the bioactive fertilizer is applied, the absorption of water and various nutrient elements such as nitrogen, phosphorus, potassium, calcium, magnesium, sulfur, iron, manganese, copper, zinc, nickel and the like by a plant root system can be obviously improved, the growth of nursery stocks is promoted, the number of lateral roots is increased by 20%, the height of seedlings and the ground diameter are increased by 25%, the survival rate of afforestation is improved by more than 15%, and the biomass is increased by 30-50%; meanwhile, the tolerance of the plants to drought, saline-alkali, barren and other environments and the capability of resisting soil-borne diseases and insect pests can be improved, the morbidity is reduced by about 25 percent, and the use of pesticides is reduced; activating beneficial microorganisms in rhizosphere soil; the photosynthesis is enhanced, and the carbon sequestration capacity of the plants is improved by more than 30 percent; the quality of the nursery stock is optimized, and the market value is increased.|[0037] In addition, when the product is applied to afforestation in an environment pollution area, after mycorrhizal fungi and plants are formed together, the degradation and conversion capacity of pollutants can be improved through the co-metabolism, the stress of the pollutants in areas such as abandoned fields, petroleum, heavy metal polluted soil, garbage mountains and the like in a mining area to trees is relieved, the afforestation survival rate is improved, and the polluted and damaged environment is repaired. Therefore, the mycorrhizal fertilizer is an environment-friendly agriculture and forestry technology, reduces the use of chemical pollutants while achieving high yield, promotes the degradation and removal of pollutants in soil, and maintains a healthy soil system. After once application, the forest tree can be benefited for the whole life, the management is simple, the cost of the forest is saved, and the environmental quality is improved. The application of the mycorrhizal biofertilizer is a development direction of green industry in the future and is also one of effective ways for realizing sustainable development of forestry.|[0038] The bioactive fertilizer taking poplar branches and fallen leaves as raw materials and the application method thereof provided by the invention are thoroughly introduced, the principle and the implementation mode of the invention are explained by applying specific examples, and the description of the examples is only used for helping to understand the method and the core idea of the invention; while the invention has been described in detail and with reference to specific embodiments thereof, it will be apparent to one skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention as defined by the appended claims. (CN103483019)|TECHNICAL FIELD|[0002] The invention relates to an active fertilizer and an application method thereof, in particular to a biological active fertilizer taking branches and fallen leaves of poplar as raw materials and an application method thereof.|BACKGROUND ART|[0004] The mycorrhiza fertilizer is a novel efficient, nontoxic, green and pollution-free biological fertilizer, can meet the requirements of agriculture and forestry product production and ecological protection, and has wide market prospect.|[0005] Mycorrhiza research has been on for over 100 years since the creation of mycorrhiza by Frank, a german plant pathologist in 1885. The mycorrhizal fungi have huge hypha systems and are tightly connected with plant root systems into a whole to form mycorrhiza, are the most widely distributed and important symbionts in the biological world, and have important significance for promoting the exchange and transmission of substances, energy and information among organisms in various ecological systems. Meanwhile, the method has profound economic, social and ecological significance for keeping ecological balance and sustainable development, protecting biological diversity, stabilizing an ecological system and promoting agriculture, forestry and animal husbandry production.|[0006] The huge mycelium spread in the soil is a main absorption organ of mycorrhiza, after the plant forms the mycorrhiza, the density of the absorbed root is increased, the root form is changed, the mycelium can go deep into soil and rock fine cracks which cannot be reached by the original plant root system, the absorption range of water and nutrients of the plant is expanded to a great extent, and therefore the biomass of the plant is improved. The mycorrhizal fungi can also activate mineral elements in soil and promote the absorption of nutrient elements by plant roots, especially the absorption of phosphorus with poor mobility and mineral elements such as zinc, copper and the like. The formation of mycorrhiza can reduce the permanent withering point of the plant and improve the drought resistance and the water utilization efficiency of the plant. In addition, the mycorrhizal fungi are inoculated to the plants, the resistance of the plants in the adverse environment can be enhanced, the survival rate of the plants is improved, the barren resistance, cold resistance and saline and alkaline resistance of the plants are enhanced, and after the mycorrhizal fungi and the root systems of the plants form mycorrhiza, the plant diseases, especially plant insect pests such as soil-borne pathogenic fungi, cyst nematodes, root knot nematodes and the like can be greatly reduced. Extracellular glycoprotein secreted by mycorrhiza is combined with hypha network, which is beneficial to the formation of soil aggregate structure, can improve soil stability, maintain soil porosity, ensure good farming condition and ventilation condition, fix organic matters in soil and improve carbon reserve in soil. The mycorrhiza can also reduce the pollution to the soil environment and the adverse effect to plants caused by heavy metal, organic pollutant, radioactive elements and the like, plants using the mycorrhiza fertilizer can absorb more heavy metal and organic pollutant than unused plants without toxicity, the organic acid secreted by the mycorrhiza fertilizer can complex the pollutant, thereby reducing the toxicity of the plant, simultaneously reducing the transportation of the pollutant from the root to the overground part, being an important storage warehouse for fixing the pollutant in the soil and having great value in pollutant degradation.|[0007] At present, the mycorrhizal fungi agents are produced by companies in many countries and are widely applied, such as the United states, Europe, Japan, Taiwan and the like. The method is mainly used for transplanting plants, such as flowers, fruit trees, greening trees and the like.|[0008] A mycorrhizal fungi agent- -rootgrowth (TM) for arid areas is researched and developed in East of Eden Plants seedling culture center in England, the fungi agent contains at least 5 mycorrhizal fungi, and can adapt to water stress, and the survival rate of seedlings can be improved by inoculating the fungi agent. The tissue Fungi PerfectR authorized in Washington, USA also has a plurality of mycorrhizal Fungi agent products, wherein the Plant SuccessTM Tabs contain 12 kinds of endophytic and exogenous mycorrhizal Fungi, and the Fungi agent can promote the growth of plants and root systems, improve the absorption of nutrients and water and reduce the use of fertilizers.|[0009] Although most mycorrhizal fungi can infect various tree species and can adapt to complex environmental conditions, the effect of achieving twice the result with half the effort can be achieved only by following the principle of being suitable for trees as much as possible in the using process. Foreign bacterial manure technology is mature and has been popularized and applied in many fields, however, foreign soil conditions and common greening tree species are greatly different from those in China, and foreign bacterial manure is not always effective for the common greening tree species in China, such as Chinese pine, and is unknown whether to cause environmental problems such as ecological invasion. In addition, the price is high, and the popularization in the garden greening of China is difficult.|[0010] The Pt mycorrhizal inoculant developed by China forestry science research institute, namely the Jianbao, has single species, the effective bacteria are mainly puffball species, the application range is narrow, and the huge requirements of the current landscaping can not be met.|DISCLOSURE|[0011] Disclosure of Invention|[0012] The invention aims to solve the problems, and the invention provides the bioactive fertilizer which takes poplar branches and fallen leaves as raw materials, can effectively promote the growth of pine and oak trees, has simple and convenient use method and low cost, obviously improves the activity of plant root systems after being used, improves soil, enhances the disease resistance and stress resistance of plants, and improves the survival rate of mycorrhiza and the application method thereof.|[0013] In order to achieve the purpose, the invention adopts the technical scheme that: a biological active fertilizer taking poplar branches and fallen leaves as raw materials and an application method thereof are disclosed, wherein the active ingredients of the fertilizer take crushed poplar branches and fallen leaves and vermiculite as main raw materials, and the crushed poplar branches and fallen leaves and the vermiculite are mixed according to the volume ratio of 2: 1, mixing, then mixing with an MMN liquid culture medium, culturing at a constant temperature of 25 ℃ for 15 days, inoculating various ectomycorrhizal fungi, when hyphae grow over the culture bag for standby, uniformly mixing with biological activated carbon, a biological organic fertilizer, a water-retaining agent and a biological activity promoting component under an aseptic condition, wherein the biological activated carbon accounts for 15% of the total volume of the biological mycorrhizal preparation, the biological organic fertilizer accounts for 25% of the total volume of the biological mycorrhizal preparation, the addition amount of the water-retaining agent is 5% of the total volume of the biological mycorrhizal preparation, and the biological activity promoting component accounts for 1% of the total volume of the biological mycorrhizal preparation, so that the solid biological myco.|[0014] Preferably, there are three methods of administration,|[0015] the direct application method comprises the following steps: during seedling transplanting and field planting, annular ditches are dug around root systems, the depth is proper for exposing absorbed roots, microbial inoculum fertilizer is scattered into the ditches and is uniformly mixed with soil, the microbial inoculum fertilizer is contacted with the root systems as much as possible, then soil is covered, watering is carried out, and the using amount is calculated by applying 150g of the fertilizer per 2.5 centimeters of the diameter of a tree trunk;|[0016] secondly, a liquid irrigation method: when the nursery stock is transplanted and planted, annular ditches are dug around the root system, the depth is suitable for exposing and absorbing roots, solid microbial inoculum fertilizer is diluted by 30-40 times by adding water, 30-40kg of water is added into 1kg of microbial inoculum, the mixture is uniformly stirred and poured into soil, and the using amount is calculated by applying 1 liter of water according to the diameter of each 2.5 cm of the tree trunk;|[0017] ③ matrix soil method: when the seedlings are transplanted and planted, the seedlings are applied according to the size of a container by 3 g/L, and the best application is spring and autumn.|[0018] Compared with the prior art, the invention has the advantages that: the bioactive fertilizer produced by the invention can be widely applied to landscaping engineering of various commonly used afforestation tree species such as coniferae, fagaceae, salicaceae, betulinaceae and the like in northern areas of China, can obviously improve the absorption of plant roots to water and various nutrient elements such as nitrogen, phosphorus, potassium, calcium, magnesium, sulfur, iron, manganese, copper, zinc, nickel and the like, promotes the growth of seedlings, can improve the tolerance of plants to environments such as drought, saline-alkali and infertile and the capability of resisting soil-borne diseases and insect pests, and reduces the use of pesticides; activating beneficial microorganisms in rhizosphere soil; enhancing photosynthesis and improving carbon fixation capacity of plants; the quality of the nursery stock is optimized, and the market value is increased. In addition, after the mycorrhizal fungi and the plants are formed together, the degradation and conversion capacity of pollutants can be improved through the co-metabolism, the stress of the pollutants in mining area waste land, petroleum, heavy metal polluted soil, garbage mountain and other areas to trees is relieved, the afforestation survival rate is improved, and the polluted and damaged environment is repaired. The application of the mycorrhizal biofertilizer is a development direction of green industry in the future and is also one of effective ways for realizing sustainable development of forestry.|INVENTION MODE|[0019] Detailed Description|[0020] The present invention will be further explained below,|[0021] example (b): a bioactive fertilizer using branches and fallen leaves of poplar as raw materials and its application method are disclosed, which comprises the following steps, using the crushed branches and fallen leaves of poplar and vermiculite as main raw materials,|[0022] sieving vermiculite, and taking a part with the particle size larger than 1mm for later use;|[0023] crushing branches and fallen leaves of the poplar, and sieving to obtain parts with the grain size of 1-10 mm for later use;|[0024] thirdly, putting the screened vermiculite and the crushed poplar branches into an autoclave respectively for sterilization treatment, cooking for 2 hours at 121 ℃, spreading the materials after cooking, and cooling;|[0025] fourthly, mixing the crushed poplar branches and vermiculite according to a volume ratio of 2: 1, and mixing the mixture with an MMN liquid culture medium, wherein the mass ratio of the materials to the liquid culture medium is 1: 1.2-1.5, and after uniformly stirring, tightly holding by hand to allow liquid to seep out, wherein each liter of MMN liquid culture medium comprises the following components: CaCl20.05g;MgSO4 0.15g;NaCl 0.025g;FeCl3 (1%)1.2ml;KH2PO40.5 g; VitamibB1 (thiamine) 100 μ g; (NH)4)2HPO40.25 g; peptone (12 Be') 100 ml; 10-15g of Glucose; 0.2g of citric acid; 900ml of distilled water; pH5.5 or so;|[0026] fifthly, filling the mixed materials into a polyethylene culture bag (17 x 33cm), plugging a cotton plug or a silica gel plug, tying the cotton plug or the silica gel plug by a rubber band, and sterilizing the mixture for 30min at the temperature of 121 ℃;|[0027] sixthly, after the culture bags (17 x 33cm) filled with the materials are cooled to room temperature, inoculating various ectomycorrhizal fungi in an ultra-clean workbench or a sterile room or a sterile environment, wherein the inoculation amount of each bag is 5-10%, and the various ectomycorrhizal fungi are inoculated into bolete pachychnos (Suillus grevillei), bolete fusca (Suillusluteus), bolete edulis (Boletus edulis), Boletus ruducens (Xerocomuschrysenton), Boletus rugosus (Gomphidius roseus) and cercospora erythraea (Lacca laccata);|[0028] seventhly, culturing in a greenhouse or an incubator at 25 ℃ in a dark place, and growing the whole bag after 15 days;|[0029] the cultured mycorrhizal fungi which are taken as main bioactive substances are mixed with the biological active carbon and the organic fertilizer according to the volume ratio of 12: 3: 5, uniformly mixing, adding the biological water-retaining agent according to 5 per mill of the mass of the mixture, adding the biological activity growth promoting component according to 1 per mill of the mass of the mixture, and uniformly mixing to prepare the microbial inoculum fertilizer;|[0030] ninthly, after being packaged, the product is stored in a shady and cool place or a refrigerator at 4 ℃.|[0031] There are three methods of application of the present invention,|[0032] the direct application method comprises the following steps: when the nursery stock is transplanted and planted, annular ditches are dug around the root system to a depth suitable for exposing absorbed roots, microbial inoculum fertilizer is scattered into the ditches and is uniformly mixed with soil, the fertilizer is contacted with the root system as much as possible, then soil is covered, and watering is carried out, wherein the using amount is calculated by applying 150g per 2.5 cm of the diameter of the trunk.|[0033] Secondly, a liquid irrigation method: when the nursery stock is transplanted and planted, annular ditches are dug around the root system, the depth is suitable for exposing and absorbing roots, solid microbial inoculum fertilizer is diluted by 30-40 times by adding water, 30-40kg of water is added into 1kg of microbial inoculum, the mixture is uniformly stirred and poured into soil, and the using amount is calculated by applying 1 liter of water according to the diameter of each 2.5 cm of the tree trunk.|[0034] ③ matrix soil method: when the nursery stock is transplanted and planted, the microbial inoculum fertilizer is applied according to the size of a container by 3 g/L, for example, 15g is added into a 5L flowerpot, and the best is spring and autumn when the microbial inoculum is applied. In summer, the cool morning or evening should be selected to avoid the high temperature weather.|[0035] After application, mycorrhiza can be formed in 2-3 months generally, the infection rate of the mycorrhiza can reach more than 80%, and the growth promoting effect is obvious after 1 year.|[0036] The biological active fertilizer produced by the invention can be widely applied to landscaping engineering of various commonly used afforestation tree species in northern China, such as coniferae, fagaceae, salicaceae, betulinaceae and the like. After the bioactive fertilizer is applied, the absorption of water and various nutrient elements such as nitrogen, phosphorus, potassium, calcium, magnesium, sulfur, iron, manganese, copper, zinc, nickel and the like by a plant root system can be obviously improved, the growth of nursery stocks is promoted, the number of lateral roots is increased by 20%, the height of seedlings and the ground diameter are increased by 25%, the survival rate of afforestation is improved by more than 15%, and the biomass is increased by 30-50%; meanwhile, the tolerance of the plants to drought, saline-alkali, barren and other environments and the capability of resisting soil-borne diseases and insect pests can be improved, the morbidity is reduced by about 25 percent, and the use of pesticides is reduced; activating beneficial microorganisms in rhizosphere soil; the photosynthesis is enhanced, and the carbon sequestration capacity of the plants is improved by more than 30 percent; the quality of the nursery stock is optimized, and the market value is increased.|[0037] In addition, when the product is applied to afforestation in an environment pollution area, after mycorrhizal fungi and plants are formed together, the degradation and conversion capacity of pollutants can be improved through the co-metabolism, the stress of the pollutants in areas such as abandoned fields, petroleum, heavy metal polluted soil, garbage mountains and the like in a mining area to trees is relieved, the afforestation survival rate is improved, and the polluted and damaged environment is repaired. Therefore, the mycorrhizal fertilizer is an environment-friendly agriculture and forestry technology, reduces the use of chemical pollutants while achieving high yield, promotes the degradation and removal of pollutants in soil, and maintains a healthy soil system. After once application, the forest tree can be benefited for the whole life, the management is simple, the cost of the forest is saved, and the environmental quality is improved. The application of the mycorrhizal biofertilizer is a development direction of green industry in the future and is also one of effective ways for realizing sustainable development of forestry.|[0038] The bioactive fertilizer taking poplar branches and fallen leaves as raw materials and the application method thereof provided by the invention are thoroughly introduced, the principle and the implementation mode of the invention are explained by applying specific examples, and the description of the examples is only used for helping to understand the method and the core idea of the invention; while the invention has been described in detail and with reference to specific embodiments thereof, it will be apparent to one skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention as defined by the appended claims. Family Number|(59506227)|59506227|Abstract|(CN103483019 A)|The invention discloses a biological active fertilizer taking the branches and fallen leaves of poplar as raw materials and an application method thereof . The effective component of the biological active fertilizer takes the branches and fallen leaf crushed substances of the poplar and vermiculite as main raw materials . The preparation method comprises the following steps of : mixing the branches and fallen leaf crushed substances of the poplar and the vermiculite according to the volume ratio of 2 : 1, and then mixing into MMN liquid culture medium ; inoculating multiple ectomycorrhizal fungus , and then uniformly mixing with biological active carbon , a biological organic fertilizer , a water retention agent and a biological active growth - promoting component under an aseptic condition to obtain a solid biological mycorrhiza formulation . Compared with the traditional biological fertilizer , the biological active fertilizer disclosed by the invention can obviously enhance the absorption of multiple nutrient elements of a plant root system , promote the growth of a seedling , enhance the tolerance and soil - borne diseases and insect pests resistant capacity of a plant on a drought environment , a saline - alkali environment , an impoverished environment , and the like , activate the beneficial microbes contained in rhizosphere soil , enhance the photosynthesis , enhance the carbon sequestration capacity of the plant , optimize the seedling quality and increase the market value . |IPC codes|(CN103483019 A)|A01C - 021/00 | Basic materials chemistry|Other special machines A01C-021/00|C05F-011/00|C05F-011/08 A01C-021/00|C05F-011/00|C05F-011/08 CN117730750|CN120642719|CN116711742|CN114766318|CN114213164|CN112042475|CN109769568|CN110604048B|CN105993273|CN104130034|CN103936488B CN117730750 109015860 WHO=Examiner SELF=N CAT=Y|CN120642719 116007371 WHO=Examiner SELF=N CAT=A|CN116711742 106443838 WHO=Examiner SELF=N CAT=A|CN114766318 100986202 WHO=Examiner SELF=N CAT=A|CN114213164 99254265 WHO=Examiner SELF=N CAT=A|CN112042475 91795422 WHO=Examiner SELF=N CAT=A|CN109769568 84564570 WHO=Examiner SELF=N CAT=A|CN110604048B 87061971 WHO=Examiner SELF=N CAT=A|CN105993273 74364205 WHO=Examiner SELF=N CAT=A|CN104130034 67886123 WHO=Examiner SELF=N CAT=A|CN103936488B 66830650 WHO=Examiner SELF=N CAT=A CN102660291 CN102660291 7880583 WHO=Examiner SELF=N 梁军等: &quot;根际微生态保健剂对杨树生长及抗病性的效应&quot;, 《南京林业大学学报(自然科学版)》, vol. 29, no. 5, 30 September 2005 (2005-09-30), pages 45 - 49 CN102660291 REVOKED (CN103483019)|REVOKED DEAD (CN103483019)|DEAD (CN103483019)|LEGAL DETAILS FOR CN103483019|Actual or expected expiration date=2019-08-23|Legal state=DEAD|Status=REVOKED|Event publication date=2013-08-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201310380093|Application date=2013-08-28|Standardized application number=2013CN-0380093|Event publication date=2014-01-01|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN103483019|Publication stage code=A|Publication date=2014-01-01|Standardized publication number=CN103483019|Event publication date=2014-01-01|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2014-04-02|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2019-08-23|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjkyurexl8BLN1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=aWOP5%252FHW4cFKx7k1bJ7MDpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN103483019)|NAME=CUI MING|NAME=ZHOU JINXING|NAME=YU MENG|NAME=QIN YONGSHENG|NAME=WANG XIAOPING|NAME=LIU YUGUO 0 1 Titre: (CN103483019)|Biological active fertilizer taking branch and fallen leaf of poplar as raw materials and application method thereof Résumé: (CN103483019)|The invention discloses a biological active fertilizer taking the branches and fallen leaves of poplar as raw materials and an application method thereof. The effective component of the biological active fertilizer takes the branches and fallen leaf crushed substances of the poplar and vermiculite as main raw materials. The preparation method comprises the following steps of: mixing the branches and fallen leaf crushed substances of the poplar and the vermiculite according to the volume ratio of 2:1, and then mixing into MMN liquid culture medium; inoculating multiple ectomycorrhizal fungus, and then uniformly mixing with biological active carbon, a biological organic fertilizer, a water retention agent and a biological active growth-promoting component under an aseptic condition to obtain a solid biological mycorrhiza formulation. Compared with the traditional biological fertilizer, the biological active fertilizer disclosed by the invention can obviously enhance the absorption of multiple nutrient elements of a plant root system, promote the growth of a seedling, enhance the tolerance and soil-borne diseases and insect pests resistant capacity of a plant on a drought environment, a saline-alkali environment, an impoverished environment, and the like, activate the beneficial microbes contained in rhizosphere soil, enhance the photosynthesis, enhance the carbon sequestration capacity of the plant, optimize the seedling quality and increase the market value. 94 Abstract gpt-4o-mini no The article focuses on a biological active fertilizer using plant materials and does not address accelerated weathering or CO₂ capture.
94 CN202311742439 CN202311742439 CN117720108 108917837 CN117720108 A 2024-03-19 [CN117720108] 2023-12-18 2023-12-18 2024-03-19 (CN117720108)|2025-06-13 (CN117720108)|Silicon carbide waste recovery process (CN117720108)|The invention relates to a silicon carbide waste recovery process applied to the technical field of silicon carbide, which comprises the following steps: step 1, firstly, breaking blocky silicon carbide waste into small blocks with fist sizes, and then putting the silicon carbide waste into a crushing mechanism for crushing treatment; step 2, adjusting and operating crushing equipment to crush the silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the mixture into a quartz boat, and closing a cover for later use; and 3, preparing a tube furnace with an air injection hole and an air exhaust hole, introducing high-purity oxygen, putting the quartz boat filled with silicon carbide in the step 2 into the tube furnace, carrying out high-temperature oxidation decarburization, cooling the tube furnace, and taking out the quartz boat to obtain decarburized silicon carbide, so that the silicon carbide waste is crushed into particles with different sizes, and the silicon carbide waste is obtained. And different particles are mixed and put into the quartz boat, so that compared with fine placement of the particles, gaps among the particles are effectively enlarged, and the carbon removal effect of the silicon carbide waste is effectively improved. ZHENGZHOU HENGSHENG TECHNOLOGY (CN117720108)|ZHENGZHOU HENGSHENG TECHNOLOGY Co.,Ltd. ([CN]) SUN SHAOPENG|WANG JIFENG|SHAO BO|LI LONG|LIU PENGHAO|FAN LILI|XU DENGWAN|LI XINGYUAN (CN117720108)|SUN SHAOPENG|WANG JIFENG|SHAO BO|LI LONG|LIU PENGHAO|FAN LILI|XU DENGWAN|LI XINGYUAN (CN117720108)|LI ZHIQIANG;Zhengzhou Yichuang Intellectual Property Agency (Special General Partnership)|Reg. Nb: 41138|ZHANG CEN;Zhengzhou Yichuang Intellectual Property Agency (Special General Partnership)|Reg. Nb: 41138 (CN117720108)|As a still further improvement of the present application, the constant temperature decarburization temperature of the tube furnace in the third step was 500℃and oxygen was injected into the tube furnace at a pressure value of 100kPa to 200kPa, and the oxygen purity was 99.9%. As the still further improvement of this application, the crushing apparatus who uses of step one includes the equipment organism, the top fixedly connected with urceolus of equipment organism, quartz boat has been placed to the bottom export of urceolus, the inside rotation of urceolus is connected with screening inner tube, the inside both ends of screening inner tube rotate respectively and are connected with fixed roller and movable roller, and fixed roller corresponds with the movable roller level, the inner wall fixedly connected with of screening inner tube promotes the page, and promote the page and be the slope setting, the carborundum waste material of pouring screening inner tube is smashed by fixed roller and movable roller, carborundum granule after the breakage is collected by the urceolus through screening inner tube, and put into quartz boat, and the waste material carborundum that is not broken completely passes through the page of promoting, cooperate the rotation of screening inner tube, pass through fixed roller and movable roller again and smash, effectively improve carborundum's crushing efficiency.|As the still further improvement's of this application supplement, braced frame's top one end fixedly connected with telescopic cylinder, telescopic cylinder's output rotates with the outer end of movable roller to be connected, promotes movable roller translation through telescopic cylinder, changes the interval of fixed roller and movable roller, is convenient for adjust the crushing effect of carborundum, realizes the carborundum of different granule sizes and handles. As another improvement of the application, the surface of the screening inner cylinder is provided with the filter screen holes, the filter screen holes are divided into a plurality of groups according to the size of the mesh, the filter screen holes of the groups are sequentially and incrementally arranged, the filter screen holes of different sizes realize the screening of silicon carbide particles of different sizes, and the extraction of silicon carbide particles of different sizes is realized. As the supplementary of another improvement of this application, the equal swing joint in both ends of screening inner tube has the carousel circle, fixedly connected with keeps off the baffle between the outer lane of two carousel circles, keeps off the baffle and hugs closely the contact with the outer port of filter screen hole, and the position of baffle at screening inner tube outer wall is adjusted through carousel circle rotation, shields the filter screen hole, adjusts the duty ratio of different filter screen holes to adjust the screening ratio of not equidimension carborundum granule. As a further improvement supplement of this application, threaded connection has the lock bolt between carousel circle and the screening inner tube, and the quantity of fender baffle corresponds with the group number of filter screen hole, and keeps off the baffle setting between two adjacent groups filter screen holes, utilizes the lock bolt to lock the state of carousel circle, effectively improves the stability of fender baffle. As another improvement of this application, the equal fixedly connected with in both ends of fender baffle extend the membrane, and extend the one end fixedly connected with spool piece of membrane to extend the membrane and be the rolling form setting with spool piece as the center, the inside of spool piece is inlayed and is had the magnet that adsorbs with screening inner tube and be connected, realizes the outside extension of fender baffle through expanding the extension membrane, effectively improves the shielding effect of fender to the filter screen hole, through the absorption of spool piece and screening inner tube, effectively improves the adhesion effect of extension membrane and screening inner tube.| (CN117720108)|1. A silicon carbide waste recycling process is characterized in that: the method comprises the following specific steps:step one: firstly, breaking massive silicon carbide waste into small blocks with the size of a fist, and then putting the silicon carbide waste into a breaking mechanism for breaking;step two: adjusting and operating crushing equipment to crush silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the silicon carbide particles into a quartz boat, and sealing a cover for standby;step three: preparing a tube furnace with an air injection hole and an air suction hole, introducing high-purity oxygen, putting the quartz boat filled with silicon carbide in the second step into the tube furnace, heating to 400-600 ℃, performing high-temperature oxidation and carbon removal at constant temperature for 2-5 hours, cooling the tube furnace, and taking out the quartz boat to obtain decarburized silicon carbide.| (CN117720108)|In order to solve the problems, the invention provides a silicon carbide waste recycling process, which comprises the following specific steps:|The invention relates to a silicon carbide waste recycling process applied to the technical field of silicon carbide, which comprises the following steps: firstly, breaking massive silicon carbide waste into small blocks with the size of a fist, and then putting the silicon carbide waste into a breaking mechanism for breaking; step two: adjusting and operating crushing equipment to crush silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the silicon carbide particles into a quartz boat, and sealing a cover for standby; step three: preparing a tube furnace with an air injection hole and an air suction hole, introducing high-purity oxygen, placing the quartz boat filled with silicon carbide in the second step into the tube furnace, performing high-temperature oxidation and decarbonization, cooling the tube furnace, and then taking out the quartz boat to obtain decarbonized silicon carbide, crushing silicon carbide waste into particles with different sizes, mixing the different particles, placing the particles into the quartz boat, and effectively increasing gaps among the particles compared with the fine placement of the particles, thereby effectively improving the carbon removal effect of the silicon carbide waste. The invention relates to a silicon carbide waste recycling process, in particular to a silicon carbide waste recycling process applied to the technical field of silicon carbide.| (CN117720108)|SILICON CARBIDE(100,104)|QUARTZ BOAT(100,32)|SILICON CARBIDE WASTE RECYCLING(100,10)|WASTE RECYCLING(100,10)|WASTE RECYCLING(100,6)|CAROUSEL CIRCLE(88,4)|FENDER BAFFLE(82,3)|EQUIDIMENSION CARBORUNDUM(66,1)|CARBORUNDUM CRUSHING(65,1)|SILICON CARBIDE PARTICLE(59,28)|FENDER BAFFLE STABILITY(58,1)|CARBORUNDUM GRANULE(57,1)|EQUIPMENT ORGANISM URCEOLUS(53,1)|MOVEABLE ROLLER(49,27)|SILICON CARBIDE WASTE(47,28)|EXTENSION MEMBRANE(45,2)|CAROUSEL CIRCLE OUTER LANE(44,1)|SCREENING INNER TUBE(43,10)|SPOOL PIECE ABSORPTION(42,1)|SPOOL PIECE(41,2)|SCREENING INNER CYLINDER(40,21)|EQUIPMENT LIFE FORM(39,3)|CAROUSEL CIRCLE ROTATION(39,1)|BREAKING(38,8)|BAFFLE(38,3)|GRANULE SIZE CARBORUNDUM(37,1)|MOVEABLE ROLLER TRANSLATION(37,1)|TUBE FURNACE(36,18)|OXYGEN PURITY(35,3)|DECARBURIZED SILICON CARBIDE(33,3)|FENDER OUTSIDE EXTENSION(33,1)|FIXING ROLLER(31,23)|CRUSHING(31,9)|PARTICLE FINE PLACEMENT(31,2)|URCEOLUS(30,3)|SLOPE SETTING(29,1)|URCEOLUS INSIDE ROTATION(29,1)|LIFTING PAGE(28,6)|DECARBONIZATION(28,1)|AIR SUCTION(26,4)|EXTENSION FILM(25,5)|SPOOL(25,2)|SCREEN RATIO(25,1)|TELESCOPIC CYLINDER(24,9)|FIST SIZE(24,4)|STANDBY(24,4)|BREAKAGE(23,1)|FINE PLACEMENT(22,3)|BLOCKING PLATE(22,2)|GRANULE SIZE(22,1)|OUTSIDE LANE(22,1)|SIZE SILICON CARBIDE PARTICLE(21,3)|ROLLING(21,1)|MAGNET(20,3)|EQUAL SWING(20,1)|FENDER(20,1)|OUTSIDE EXTENSION(20,1)|REMOVING CARBON(19,9)|FILTER DUTY RATIO(19,1)|CARBORUNDUM(18,3)|OUTER PORT(18,3)|SCREENING(17,2)|MOVEABLE ROLLER LEVEL(17,1)|ROTATING INSIDE(17,1)|OUTER CYLINDER(16,9)|THREADED CONNECTION(16,3)|WINDING MODE(16,1)|GRANULE(15,3)|WASTE MATERIAL CARBORUNDUM(15,1)|AIR INJECTION HOLE(14,4)|ROTARY TABLE RING(14,3)|APPLICATION SUPPLEMENT(14,1)|SCREENING INNER TUBE ROTATION(14,1)|PARTICLE SIZE(13,11)|CONSTANT TEMPERATURE DECARBURIZATION TEMPERATURE(13,3)|INNER TUBE(12,3)|ADSORPTION CONNECTION(12,2)|TELESCOPIC CYLINDER OUTPUT(12,2)|DUTY RATIO(12,1)|ADJACENT GROUP(11,1)|BRACED FRAME TOP(11,1)|CARBORUNDUM WASTE MATERIAL(9,5)|CONSTANT TEMPERATURE(9,3)|PRESSURE VALUE(9,3)|SCREENING INNER BARREL SURFACE(9,1)|HIGH PURITY OXYGEN(8,4)|TOTAL VOLUME(8,3)|OUTER RING(8,2)|TURNTABLE COLLAR(8,2)|SUPPORTING FRAME(7,5)|LOCKING BOLT(7,3)|EQUIPMENT TOP(7,2)|SCREENING INNER CYLINDER SURFACE(7,2)|CLOSE CONTACT(7,1)|STEP THREE(6,4)|GRANULE FINE PLACEMENT(6,1)|WASTE PARTICLE CRUSHING TREATMENT(6,1)|INNER WALL(5,3)|MESH NUMBER(5,2)|TURNTABLE RING(5,2)|SCREENING INNER TUBE END(5,1)|SILICON CARBIDE CRUSHING REQUIREMENT(5,1)|WASTE MATERIAL(4,9)|GRINDING(4,4)|HIGH TEMPERATURE OXIDATION(4,4)|FILTER HOLE(4,2)|FIXED ROLLER INSTALLATION STABILITY(4,2)|GAS CIRCULATION(4,2)|MOVEABLE ROLLER OUTER END(4,2)|CAROUSEL ACTION(4,1)|ORGANIC IMPURITY(4,1)|PARTICLE SCREENING RATIO(4,1)| (CN117720108)|1. A silicon carbide waste recycling process is characterized in that: the method comprises the following specific steps:|step one: firstly, breaking massive silicon carbide waste into small blocks with the size of a fist, and then putting the silicon carbide waste into a breaking mechanism for breaking;|step two: adjusting and operating crushing equipment to crush silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the silicon carbide particles into a quartz boat, and sealing a cover for standby;|step three: preparing a tube furnace with an air injection hole and an air suction hole, introducing high-purity oxygen, putting the quartz boat filled with silicon carbide in the second step into the tube furnace, heating to 400-600 ℃, performing high-temperature oxidation and carbon removal at constant temperature for 2-5 hours, cooling the tube furnace, and taking out the quartz boat to obtain decarburized silicon carbide.|2. A silicon carbide waste recycling process according to claim 1, wherein: and in the second step, the silicon carbide particles are filled in the quartz boat and account for 1/3-2/3 of the total volume inside the quartz boat.|3. A silicon carbide waste recycling process according to claim 1, wherein: the constant temperature decarburization temperature of the tube furnace in the third step is 500 ℃, the oxygen is injected into the tube furnace at a pressure value of 100kPa-200kPa, and the oxygen purity is 99.9%.|4. A silicon carbide waste recycling process according to claim 1, wherein: the crushing mechanism used in the first step comprises an equipment body (1), the top of the equipment body (1) is fixedly connected with an outer cylinder (101), a quartz boat is placed at the bottom outlet of the outer cylinder (101), a screening inner cylinder (2) is rotationally connected to the inner part of the outer cylinder (101), a fixed roller (201) and a movable roller (202) are rotationally connected to the two ends of the inner part of the screening inner cylinder (2) respectively, the fixed roller (201) horizontally corresponds to the movable roller (202), a lifting page (203) is fixedly connected to the inner wall of the screening inner cylinder (2), and the lifting page (203) is obliquely arranged.|5. A silicon carbide waste recycling process according to claim 4, wherein: the front end and the rear end of the equipment body (1) are fixedly connected with supporting frames (102), and the fixed roller (201) and the movable roller (202) are movably connected with the supporting frames (102).|6. A silicon carbide waste recycling process according to claim 5, wherein: the top one end fixedly connected with telescopic cylinder (103) of braced frame (102), the output of telescopic cylinder (103) is connected with the outer end rotation of movable roller (202).|7. A silicon carbide waste recycling process according to claim 4, wherein: the surface of the screening inner barrel (2) is provided with filter screen holes (3), the filter screen holes (3) are divided into a plurality of groups according to the mesh number, and the filter screen holes (3) of the plurality of groups are sequentially arranged in an increasing mode.|8. A silicon carbide waste recycling process according to claim 7, wherein: both ends of the screening inner cylinder (2) are movably connected with rotary table rings (301), a baffle plate (302) is fixedly connected between the outer rings of the rotary table rings (301), and the baffle plate (302) is in close contact with the outer port of the filter screen hole (3).|9. A silicon carbide waste recycling process according to claim 8, wherein: the rotary table ring (301) is in threaded connection with the screening inner cylinder (2) and is provided with locking bolts (303), the number of the blocking plates (302) corresponds to the number of groups of the filter screen holes (3), and the blocking plates (302) are arranged between two adjacent groups of the filter screen holes (3).|10. A silicon carbide waste recycling process according to claim 9, wherein: the two ends of the baffle plate (302) are fixedly connected with an extension film (4), one end of the extension film (4) is fixedly connected with a scroll plate (401), the extension film (4) is arranged in a winding mode by taking the scroll plate (401) as the center, and a magnet which is in adsorption connection with the screening inner cylinder (2) is inlaid in the scroll plate (401). (CN117720108)|TECHNICAL FIELD|[0001] The invention relates to a silicon carbide waste recycling process, in particular to a silicon carbide waste recycling process applied to the technical field of silicon carbide.|BACKGROUND ART|[0002] The waste silicon carbide products are also used in a plurality of ways after being recycled, and can be used for producing deoxidizers, refractory materials, wear-resistant materials and other products. The waste silicon carbide products can be crushed into particles by a crusher and used as deoxidizing agent in steel works, and the waste silicon carbide particles are used as deoxidizing agent, so that the steel-making cost is greatly reduced, and the method is very popular with steel enterprises. Organic impurities in the silicon carbide waste are volatile, and can not be carbonized under high temperature conditions to form carbon. The carbonaceous material is substantially identical to the carbon enriched in crystal growth. The main SiC and main impurities C and Si contained in the silicon carbide waste material are oxidized to gaseous carbon dioxide by oxidation due to the difference of oxidation temperatures at high temperature, and carbon is removed.|[0003] Chinese patent CN202111582018.3 specification discloses a recovery unit for silicon carbide long crystal waste, through the box unit that is used for storing, grinding and screening silicon carbide waste, the action of carousel can realize grinding and throw in silicon carbide waste, and the carousel has and breaks away from the locking function when not using and avoid unexpected rotation to lead to the silicon carbide waste to drop and cause the pollution, the carousel has been designed simultaneously and has promoted can return the locking and make only need operate carousel one part operation mode easy and simple to handle when using, and additionally set up structures such as screen cloth and flitch and realized the advantage that filters waste after grinding.|[0004] The silicon carbide waste materials after grinding in the invention are put into a quartz boat, and because the waste material particles put into the quartz boat are too uniform and fine, the fine waste material particles influence the gas circulation and influence the carbon removal effect of the silicon carbide waste materials.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the prior art, the invention aims to solve the technical problems that the crushing treatment of the waste particles is too uniform and fine, the gas circulation among the waste particles is influenced, and the carbon removal effect of the silicon carbide waste is influenced.|[0006] In order to solve the problems, the invention provides a silicon carbide waste recycling process, which comprises the following specific steps:|[0007] step one: firstly, breaking massive silicon carbide waste into small blocks with the size of a fist, and then putting the silicon carbide waste into a breaking mechanism for breaking;|[0008] step two: adjusting and operating crushing equipment to crush silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the silicon carbide particles into a quartz boat, and sealing a cover for standby;|[0009] step three: preparing a tube furnace with an air injection hole and an air suction hole, introducing high-purity oxygen, putting the quartz boat filled with silicon carbide in the second step into the tube furnace, heating to 400-600 ℃, performing high-temperature oxidation and carbon removal at constant temperature for 2-5 hours, cooling the tube furnace, and taking out the quartz boat to obtain decarburized silicon carbide.|[0010] In the silicon carbide waste recycling process, the silicon carbide waste is crushed into particles with different sizes, and different particles are mixed and put into the quartz boat, so that compared with the fine placement of the particles, the gap between the particles is effectively increased, and the carbon removal effect of the silicon carbide waste is effectively improved.|[0011] As a further improvement of the application, the silicon carbide particles are filled in the quartz boat in the second step, wherein the silicon carbide particles account for 1/3-2/3 of the total volume inside the quartz boat.|[0012] As a still further improvement of the present application, the constant temperature decarburization temperature of the tube furnace in the third step was 500℃and oxygen was injected into the tube furnace at a pressure value of 100kPa to 200kPa, and the oxygen purity was 99.9%.|[0013] As the still further improvement of this application, the crushing apparatus who uses of step one includes the equipment organism, the top fixedly connected with urceolus of equipment organism, quartz boat has been placed to the bottom export of urceolus, the inside rotation of urceolus is connected with screening inner tube, the inside both ends of screening inner tube rotate respectively and are connected with fixed roller and movable roller, and fixed roller corresponds with the movable roller level, the inner wall fixedly connected with of screening inner tube promotes the page, and promote the page and be the slope setting, the carborundum waste material of pouring screening inner tube is smashed by fixed roller and movable roller, carborundum granule after the breakage is collected by the urceolus through screening inner tube, and put into quartz boat, and the waste material carborundum that is not broken completely passes through the page of promoting, cooperate the rotation of screening inner tube, pass through fixed roller and movable roller again and smash, effectively improve carborundum's crushing efficiency.|[0014] As the supplement of the even further improvement of this application, both ends all fixedly connected with braced frame around the equipment organism, fixed roller and movable roller all with braced frame swing joint, effectively improve the installation stability of fixed roller and movable roller.|[0015] As the still further improvement's of this application supplement, braced frame's top one end fixedly connected with telescopic cylinder, telescopic cylinder's output rotates with the outer end of movable roller to be connected, promotes movable roller translation through telescopic cylinder, changes the interval of fixed roller and movable roller, is convenient for adjust the crushing effect of carborundum, realizes the carborundum of different granule sizes and handles.|[0016] As another improvement of the application, the surface of the screening inner cylinder is provided with the filter screen holes, the filter screen holes are divided into a plurality of groups according to the size of the mesh, the filter screen holes of the groups are sequentially and incrementally arranged, the filter screen holes of different sizes realize the screening of silicon carbide particles of different sizes, and the extraction of silicon carbide particles of different sizes is realized.|[0017] As the supplementary of another improvement of this application, the equal swing joint in both ends of screening inner tube has the carousel circle, fixedly connected with keeps off the baffle between the outer lane of two carousel circles, keeps off the baffle and hugs closely the contact with the outer port of filter screen hole, and the position of baffle at screening inner tube outer wall is adjusted through carousel circle rotation, shields the filter screen hole, adjusts the duty ratio of different filter screen holes to adjust the screening ratio of not equidimension carborundum granule.|[0018] As a further improvement supplement of this application, threaded connection has the lock bolt between carousel circle and the screening inner tube, and the quantity of fender baffle corresponds with the group number of filter screen hole, and keeps off the baffle setting between two adjacent groups filter screen holes, utilizes the lock bolt to lock the state of carousel circle, effectively improves the stability of fender baffle.|[0019] As another improvement of this application, the equal fixedly connected with in both ends of fender baffle extend the membrane, and extend the one end fixedly connected with spool piece of membrane to extend the membrane and be the rolling form setting with spool piece as the center, the inside of spool piece is inlayed and is had the magnet that adsorbs with screening inner tube and be connected, realizes the outside extension of fender baffle through expanding the extension membrane, effectively improves the shielding effect of fender to the filter screen hole, through the absorption of spool piece and screening inner tube, effectively improves the adhesion effect of extension membrane and screening inner tube.|[0020] To sum up, through putting into crushing mechanism with the carborundum waste material in this scheme, utilize fixed roll and movable roll crushing to carry out crushing processing to the carborundum waste material, carborundum after the crushing is sieved through the filter screen hole on the screening inner tube, and the carborundum that realizes multiple granule size through the filter screen hole of equidimension is selected, collects through the urceolus and mixes and put into the quartz boat, and carborundum waste material crushing efficiency is high, compares in the fine placement of granule, effectively increases the clearance between the granule, effectively improves the carbon removal effect of carborundum waste material.|DRAWINGS DESCRIPTION|[0021] FIG. 1 is a flow chart of a first embodiment of the present application;|[0022] FIG. 2 is a comparative illustration of a quartz boat according to the first embodiment of the present application containing silicon carbide particles of different sizes;|[0023] FIG. 3 is a front perspective view of a second embodiment of the present application;|[0024] FIG. 4 is a rear perspective view of a second embodiment of the present application;|[0025] FIG. 5 is a cross-sectional view of a second embodiment of the present application;|[0026] FIG. 6 is a perspective view of a second embodiment of the sifting drum of the present application;|[0027] FIG. 7 is a perspective view of the inner barrel, turntable collar and baffle plate of the second embodiment of the present application;|[0028] FIG. 8 is a perspective view of a turntable collar and a baffle plate according to a second embodiment of the present application;|[0029] fig. 9 is a perspective view of an extension film and a roll sheet according to a second embodiment of the present application.|[0030] The reference numerals in the figures illustrate:|[0031] 1. an equipment body; 101. an outer cylinder; 102. a support frame; 103. a telescopic cylinder; 2. screening the inner cylinder; 201. a fixed roller; 202. a movable roller; 203. lifting the page; 3. a filter mesh; 301. a turntable ring; 302. a baffle plate; 303. a locking bolt; 4. an extension film; 401. and a reel sheet.|INVENTION MODE|Detailed Description|[0032] Two embodiments of the present application are described in detail below with reference to the accompanying drawings.|[0033] First embodiment:|[0034] 1-2 illustrate a silicon carbide waste recovery process, comprising the following specific steps:|[0035] step one: firstly, breaking massive silicon carbide waste into small blocks with the size of a fist, and then putting the silicon carbide waste into a breaking mechanism for breaking;|[0036] step two: adjusting and operating crushing equipment to crush silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the silicon carbide particles into a quartz boat, and sealing a cover for standby;|[0037] step three: preparing a tube furnace with an air injection hole and an air suction hole, introducing high-purity oxygen, putting the quartz boat filled with silicon carbide in the second step into the tube furnace, heating to 400-600 ℃, performing high-temperature oxidation and carbon removal at constant temperature for 2-5 hours, cooling the tube furnace, and taking out the quartz boat to obtain decarburized silicon carbide;|[0038] in the second step, the silicon carbide particles are filled in the quartz boat in an amount of 1/3-2/3 of the total volume inside the quartz boat, and as a further improvement of the application, the constant-temperature decarburization temperature of the tube furnace in the third step is 500 ℃, and oxygen is injected into the tube furnace at a pressure value of 100kPa-200kPa, wherein the oxygen purity is 99.9%;|[0039] according to the method, silicon carbide waste is crushed into particles with different sizes, the particles are mixed and placed into the quartz boat, and silicon carbide particles with different particle sizes are stacked on each other, so that compared with the placement of fine silicon carbide particles, the gaps among the particles are effectively increased, compared with the placement of large silicon carbide particles, the utilization rate of the inner space of the quartz boat is increased, and the carbon removal effect of the silicon carbide waste is effectively improved.|[0040] Second embodiment:|[0041] 3-5 show that the crushing mechanism used in the first step comprises an equipment body 1, the top of the equipment body 1 is fixedly connected with an outer cylinder 101, a quartz boat is placed at the bottom outlet of the outer cylinder 101, a screening inner cylinder 2 is rotatably connected to the inner part of the outer cylinder 101, a fixed roller 201 and a movable roller 202 are rotatably connected to the two ends of the inner part of the screening inner cylinder 2 respectively, the fixed roller 201 horizontally corresponds to the movable roller 202, a lifting page 203 is fixedly connected to the inner wall of the screening inner cylinder 2, the lifting page 203 is obliquely arranged, silicon carbide waste poured into the screening inner cylinder 2 is crushed by the fixed roller 201 and the movable roller 202, crushed silicon carbide particles are collected by the outer cylinder 101 through the screening inner cylinder 2 and put into the quartz boat, and waste silicon carbide which is not completely crushed is crushed by the lifting page 203 and is crushed again through the fixed roller 201 and the movable roller 202 in cooperation with the rotation of the screening inner cylinder 2, so that the crushing efficiency of silicon carbide is effectively improved;|[0042] when the crushing treatment of the silicon carbide waste is carried out, the silicon carbide waste is put into the screening inner cylinder 2, the silicon carbide waste is crushed by the fixed roller 201 and the movable roller 202, the crushed silicon carbide particles are taken out through the screening inner cylinder 2 and are collected by the outer cylinder 101, finally, the silicon carbide waste which is not completely crushed is put into the quartz boat, pushed by the lifting page 203, and is matched with the rotation lifting of the screening inner cylinder 2 to be crushed by the fixed roller 201 and the movable roller 202 continuously, so that the crushing effect of the silicon carbide waste is effectively improved.|[0043] 3-4 show that the front end and the rear end of the equipment body 1 are fixedly connected with the supporting frame 102, the fixed roller 201 and the movable roller 202 are movably connected with the supporting frame 102, so that the installation stability of the fixed roller 201 and the movable roller 202 is effectively improved, one end of the top of the supporting frame 102 is fixedly connected with the telescopic cylinder 103, the output end of the telescopic cylinder 103 is rotationally connected with the outer end of the movable roller 202, the movable roller 202 is pushed to translate by the telescopic cylinder 103, the distance between the fixed roller 201 and the movable roller 202 is changed, the crushing effect of silicon carbide is conveniently adjusted, and silicon carbide treatment with different particle sizes is realized;|[0044] when silicon carbide is crushed, according to the crushing requirement of silicon carbide, the telescopic cylinder 103 is operated in advance to stretch and adjust, the movable roller 202 is pushed to horizontally displace, the distance between the fixed roller 201 and the movable roller 202 is adjusted, the larger the distance between the fixed roller 201 and the movable roller 202 is, the larger the particles after crushing silicon carbide waste are, and otherwise, the smaller the distance between the fixed roller 201 and the movable roller 202 is, the smaller the particles after crushing the silicon carbide waste are, so that the crushing effect of adjusting the silicon carbide waste is realized.|[0045] 5-7 show that the surface of the screening inner cylinder 2 is provided with a plurality of groups of filter holes 3, the filter holes 3 are divided into a plurality of groups according to the mesh number, the groups of filter holes 3 are sequentially and incrementally arranged, the filter holes 3 with different sizes are used for screening silicon carbide particles with different sizes, the extraction of silicon carbide with different particle sizes is realized, both ends of the screening inner cylinder 2 are movably connected with turntable rings 301, a baffle plate 302 is fixedly connected between the outer rings of the two turntable rings 301, the baffle plate 302 is tightly contacted with the outer ports of the filter holes 3, the positions of the baffle plate 302 on the outer wall of the screening inner cylinder 2 are adjusted through the rotation of the turntable rings 301, the filter holes 3 are shielded, the proportion of the silicon carbide particles with different sizes is adjusted, locking bolts 303 are in threaded connection between the turntable rings 301 and the screening inner cylinder 2, the number of the baffle plate 302 corresponds to the group number of the filter holes 3, the baffle plate 302 is arranged between the two adjacent groups of the filter holes 3, and the state of the baffle plate 301 is locked by the locking bolts 303, so that the stability of the baffle plate 302 is effectively improved;|[0046] the screening of different silicon carbide particles is realized by utilizing the filter screen holes 3 with different sizes, as shown in fig. 6, three specifications of filter screen holes 3 are arranged in the drawing, small-sized silicon carbide is screened out by the small-sized filter screen holes 3, small-sized and medium-sized silicon carbide is screened out by the medium-sized filter screen holes 3, small-sized, medium-sized and large-sized silicon carbide is screened out by the large-sized filter screen holes 3, different filter screen holes 3 are shielded by the rotary table ring 301 for rotating the adjusting baffle plate 302, the occupied area of different filter screen holes 3 is changed, and therefore the screening ratio of the particles with different sizes is adjusted, and the mixing effect of the silicon carbide particles is effectively improved.|[0047] 8-9 show that the two ends of the baffle plate 302 are fixedly connected with an extension film 4, one end of the extension film 4 is fixedly connected with a scroll plate 401, the extension film 4 is arranged in a rolling mode by taking the scroll plate 401 as the center, a magnet which is in adsorption connection with the screening inner cylinder 2 is embedded in the scroll plate 401, the extension film 4 is unfolded to realize outward extension of the baffle plate 302, and the shielding effect of the baffle plate 302 on the filter screen hole 3 is effectively improved;|[0048] after the position of the baffle plate 302 is adjusted, the extension film 4 is rolled and unfolded through the scroll plate 401, the shielding area of the baffle plate 302 is extended outwards, the shielding effect on different filter screen holes 3 is effectively improved, and the adhesion effect of the extension film 4 and the screening inner barrel 2 is effectively improved through the adsorption of the scroll plate 401 and the screening inner barrel 2.|[0049] The scope of protection of the above-described embodiments employed in the present application is not limited to the above-described embodiments, and various changes made by those skilled in the art without departing from the spirit of the present application are still within the scope of protection of the present invention. (CN117720108)|TECHNICAL FIELD|[0001] The invention relates to a silicon carbide waste recycling process, in particular to a silicon carbide waste recycling process applied to the technical field of silicon carbide.|BACKGROUND ART|[0002] The waste silicon carbide products are also used in a plurality of ways after being recycled, and can be used for producing deoxidizers, refractory materials, wear-resistant materials and other products. The waste silicon carbide products can be crushed into particles by a crusher and used as deoxidizing agent in steel works, and the waste silicon carbide particles are used as deoxidizing agent, so that the steel-making cost is greatly reduced, and the method is very popular with steel enterprises. Organic impurities in the silicon carbide waste are volatile, and can not be carbonized under high temperature conditions to form carbon. The carbonaceous material is substantially identical to the carbon enriched in crystal growth. The main SiC and main impurities C and Si contained in the silicon carbide waste material are oxidized to gaseous carbon dioxide by oxidation due to the difference of oxidation temperatures at high temperature, and carbon is removed.|[0003] Chinese patent CN202111582018.3 specification discloses a recovery unit for silicon carbide long crystal waste, through the box unit that is used for storing, grinding and screening silicon carbide waste, the action of carousel can realize grinding and throw in silicon carbide waste, and the carousel has and breaks away from the locking function when not using and avoid unexpected rotation to lead to the silicon carbide waste to drop and cause the pollution, the carousel has been designed simultaneously and has promoted can return the locking and make only need operate carousel one part operation mode easy and simple to handle when using, and additionally set up structures such as screen cloth and flitch and realized the advantage that filters waste after grinding.|[0004] The silicon carbide waste materials after grinding in the invention are put into a quartz boat, and because the waste material particles put into the quartz boat are too uniform and fine, the fine waste material particles influence the gas circulation and influence the carbon removal effect of the silicon carbide waste materials.|DISCLOSURE|Disclosure of Invention|[0005] Aiming at the prior art, the invention aims to solve the technical problems that the crushing treatment of the waste particles is too uniform and fine, the gas circulation among the waste particles is influenced, and the carbon removal effect of the silicon carbide waste is influenced.|[0006] In order to solve the problems, the invention provides a silicon carbide waste recycling process, which comprises the following specific steps:|[0007] step one: firstly, breaking massive silicon carbide waste into small blocks with the size of a fist, and then putting the silicon carbide waste into a breaking mechanism for breaking;|[0008] step two: adjusting and operating crushing equipment to crush silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the silicon carbide particles into a quartz boat, and sealing a cover for standby;|[0009] step three: preparing a tube furnace with an air injection hole and an air suction hole, introducing high-purity oxygen, putting the quartz boat filled with silicon carbide in the second step into the tube furnace, heating to 400-600 ℃, performing high-temperature oxidation and carbon removal at constant temperature for 2-5 hours, cooling the tube furnace, and taking out the quartz boat to obtain decarburized silicon carbide.|[0010] In the silicon carbide waste recycling process, the silicon carbide waste is crushed into particles with different sizes, and different particles are mixed and put into the quartz boat, so that compared with the fine placement of the particles, the gap between the particles is effectively increased, and the carbon removal effect of the silicon carbide waste is effectively improved.|[0011] As a further improvement of the application, the silicon carbide particles are filled in the quartz boat in the second step, wherein the silicon carbide particles account for 1/3-2/3 of the total volume inside the quartz boat.|[0012] As a still further improvement of the present application, the constant temperature decarburization temperature of the tube furnace in the third step was 500℃and oxygen was injected into the tube furnace at a pressure value of 100kPa to 200kPa, and the oxygen purity was 99.9%.|[0013] As the still further improvement of this application, the crushing apparatus who uses of step one includes the equipment organism, the top fixedly connected with urceolus of equipment organism, quartz boat has been placed to the bottom export of urceolus, the inside rotation of urceolus is connected with screening inner tube, the inside both ends of screening inner tube rotate respectively and are connected with fixed roller and movable roller, and fixed roller corresponds with the movable roller level, the inner wall fixedly connected with of screening inner tube promotes the page, and promote the page and be the slope setting, the carborundum waste material of pouring screening inner tube is smashed by fixed roller and movable roller, carborundum granule after the breakage is collected by the urceolus through screening inner tube, and put into quartz boat, and the waste material carborundum that is not broken completely passes through the page of promoting, cooperate the rotation of screening inner tube, pass through fixed roller and movable roller again and smash, effectively improve carborundum's crushing efficiency.|[0014] As the supplement of the even further improvement of this application, both ends all fixedly connected with braced frame around the equipment organism, fixed roller and movable roller all with braced frame swing joint, effectively improve the installation stability of fixed roller and movable roller.|[0015] As the still further improvement's of this application supplement, braced frame's top one end fixedly connected with telescopic cylinder, telescopic cylinder's output rotates with the outer end of movable roller to be connected, promotes movable roller translation through telescopic cylinder, changes the interval of fixed roller and movable roller, is convenient for adjust the crushing effect of carborundum, realizes the carborundum of different granule sizes and handles.|[0016] As another improvement of the application, the surface of the screening inner cylinder is provided with the filter screen holes, the filter screen holes are divided into a plurality of groups according to the size of the mesh, the filter screen holes of the groups are sequentially and incrementally arranged, the filter screen holes of different sizes realize the screening of silicon carbide particles of different sizes, and the extraction of silicon carbide particles of different sizes is realized.|[0017] As the supplementary of another improvement of this application, the equal swing joint in both ends of screening inner tube has the carousel circle, fixedly connected with keeps off the baffle between the outer lane of two carousel circles, keeps off the baffle and hugs closely the contact with the outer port of filter screen hole, and the position of baffle at screening inner tube outer wall is adjusted through carousel circle rotation, shields the filter screen hole, adjusts the duty ratio of different filter screen holes to adjust the screening ratio of not equidimension carborundum granule.|[0018] As a further improvement supplement of this application, threaded connection has the lock bolt between carousel circle and the screening inner tube, and the quantity of fender baffle corresponds with the group number of filter screen hole, and keeps off the baffle setting between two adjacent groups filter screen holes, utilizes the lock bolt to lock the state of carousel circle, effectively improves the stability of fender baffle.|[0019] As another improvement of this application, the equal fixedly connected with in both ends of fender baffle extend the membrane, and extend the one end fixedly connected with spool piece of membrane to extend the membrane and be the rolling form setting with spool piece as the center, the inside of spool piece is inlayed and is had the magnet that adsorbs with screening inner tube and be connected, realizes the outside extension of fender baffle through expanding the extension membrane, effectively improves the shielding effect of fender to the filter screen hole, through the absorption of spool piece and screening inner tube, effectively improves the adhesion effect of extension membrane and screening inner tube.|[0020] To sum up, through putting into crushing mechanism with the carborundum waste material in this scheme, utilize fixed roll and movable roll crushing to carry out crushing processing to the carborundum waste material, carborundum after the crushing is sieved through the filter screen hole on the screening inner tube, and the carborundum that realizes multiple granule size through the filter screen hole of equidimension is selected, collects through the urceolus and mixes and put into the quartz boat, and carborundum waste material crushing efficiency is high, compares in the fine placement of granule, effectively increases the clearance between the granule, effectively improves the carbon removal effect of carborundum waste material.|DRAWINGS DESCRIPTION|[0021] FIG. 1 is a flow chart of a first embodiment of the present application;|[0022] FIG. 2 is a comparative illustration of a quartz boat according to the first embodiment of the present application containing silicon carbide particles of different sizes;|[0023] FIG. 3 is a front perspective view of a second embodiment of the present application;|[0024] FIG. 4 is a rear perspective view of a second embodiment of the present application;|[0025] FIG. 5 is a cross-sectional view of a second embodiment of the present application;|[0026] FIG. 6 is a perspective view of a second embodiment of the sifting drum of the present application;|[0027] FIG. 7 is a perspective view of the inner barrel, turntable collar and baffle plate of the second embodiment of the present application;|[0028] FIG. 8 is a perspective view of a turntable collar and a baffle plate according to a second embodiment of the present application;|[0029] fig. 9 is a perspective view of an extension film and a roll sheet according to a second embodiment of the present application.|[0030] The reference numerals in the figures illustrate:|[0031] 1. an equipment body; 101. an outer cylinder; 102. a support frame; 103. a telescopic cylinder; 2. screening the inner cylinder; 201. a fixed roller; 202. a movable roller; 203. lifting the page; 3. a filter mesh; 301. a turntable ring; 302. a baffle plate; 303. a locking bolt; 4. an extension film; 401. and a reel sheet.|INVENTION MODE|Detailed Description|[0032] Two embodiments of the present application are described in detail below with reference to the accompanying drawings.|[0033] First embodiment:|[0034] 1-2 illustrate a silicon carbide waste recovery process, comprising the following specific steps:|[0035] step one: firstly, breaking massive silicon carbide waste into small blocks with the size of a fist, and then putting the silicon carbide waste into a breaking mechanism for breaking;|[0036] step two: adjusting and operating crushing equipment to crush silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the silicon carbide particles into a quartz boat, and sealing a cover for standby;|[0037] step three: preparing a tube furnace with an air injection hole and an air suction hole, introducing high-purity oxygen, putting the quartz boat filled with silicon carbide in the second step into the tube furnace, heating to 400-600 ℃, performing high-temperature oxidation and carbon removal at constant temperature for 2-5 hours, cooling the tube furnace, and taking out the quartz boat to obtain decarburized silicon carbide;|[0038] in the second step, the silicon carbide particles are filled in the quartz boat in an amount of 1/3-2/3 of the total volume inside the quartz boat, and as a further improvement of the application, the constant-temperature decarburization temperature of the tube furnace in the third step is 500 ℃, and oxygen is injected into the tube furnace at a pressure value of 100kPa-200kPa, wherein the oxygen purity is 99.9%;|[0039] according to the method, silicon carbide waste is crushed into particles with different sizes, the particles are mixed and placed into the quartz boat, and silicon carbide particles with different particle sizes are stacked on each other, so that compared with the placement of fine silicon carbide particles, the gaps among the particles are effectively increased, compared with the placement of large silicon carbide particles, the utilization rate of the inner space of the quartz boat is increased, and the carbon removal effect of the silicon carbide waste is effectively improved.|[0040] Second embodiment:|[0041] 3-5 show that the crushing mechanism used in the first step comprises an equipment body 1, the top of the equipment body 1 is fixedly connected with an outer cylinder 101, a quartz boat is placed at the bottom outlet of the outer cylinder 101, a screening inner cylinder 2 is rotatably connected to the inner part of the outer cylinder 101, a fixed roller 201 and a movable roller 202 are rotatably connected to the two ends of the inner part of the screening inner cylinder 2 respectively, the fixed roller 201 horizontally corresponds to the movable roller 202, a lifting page 203 is fixedly connected to the inner wall of the screening inner cylinder 2, the lifting page 203 is obliquely arranged, silicon carbide waste poured into the screening inner cylinder 2 is crushed by the fixed roller 201 and the movable roller 202, crushed silicon carbide particles are collected by the outer cylinder 101 through the screening inner cylinder 2 and put into the quartz boat, and waste silicon carbide which is not completely crushed is crushed by the lifting page 203 and is crushed again through the fixed roller 201 and the movable roller 202 in cooperation with the rotation of the screening inner cylinder 2, so that the crushing efficiency of silicon carbide is effectively improved;|[0042] when the crushing treatment of the silicon carbide waste is carried out, the silicon carbide waste is put into the screening inner cylinder 2, the silicon carbide waste is crushed by the fixed roller 201 and the movable roller 202, the crushed silicon carbide particles are taken out through the screening inner cylinder 2 and are collected by the outer cylinder 101, finally, the silicon carbide waste which is not completely crushed is put into the quartz boat, pushed by the lifting page 203, and is matched with the rotation lifting of the screening inner cylinder 2 to be crushed by the fixed roller 201 and the movable roller 202 continuously, so that the crushing effect of the silicon carbide waste is effectively improved.|[0043] 3-4 show that the front end and the rear end of the equipment body 1 are fixedly connected with the supporting frame 102, the fixed roller 201 and the movable roller 202 are movably connected with the supporting frame 102, so that the installation stability of the fixed roller 201 and the movable roller 202 is effectively improved, one end of the top of the supporting frame 102 is fixedly connected with the telescopic cylinder 103, the output end of the telescopic cylinder 103 is rotationally connected with the outer end of the movable roller 202, the movable roller 202 is pushed to translate by the telescopic cylinder 103, the distance between the fixed roller 201 and the movable roller 202 is changed, the crushing effect of silicon carbide is conveniently adjusted, and silicon carbide treatment with different particle sizes is realized;|[0044] when silicon carbide is crushed, according to the crushing requirement of silicon carbide, the telescopic cylinder 103 is operated in advance to stretch and adjust, the movable roller 202 is pushed to horizontally displace, the distance between the fixed roller 201 and the movable roller 202 is adjusted, the larger the distance between the fixed roller 201 and the movable roller 202 is, the larger the particles after crushing silicon carbide waste are, and otherwise, the smaller the distance between the fixed roller 201 and the movable roller 202 is, the smaller the particles after crushing the silicon carbide waste are, so that the crushing effect of adjusting the silicon carbide waste is realized.|[0045] 5-7 show that the surface of the screening inner cylinder 2 is provided with a plurality of groups of filter holes 3, the filter holes 3 are divided into a plurality of groups according to the mesh number, the groups of filter holes 3 are sequentially and incrementally arranged, the filter holes 3 with different sizes are used for screening silicon carbide particles with different sizes, the extraction of silicon carbide with different particle sizes is realized, both ends of the screening inner cylinder 2 are movably connected with turntable rings 301, a baffle plate 302 is fixedly connected between the outer rings of the two turntable rings 301, the baffle plate 302 is tightly contacted with the outer ports of the filter holes 3, the positions of the baffle plate 302 on the outer wall of the screening inner cylinder 2 are adjusted through the rotation of the turntable rings 301, the filter holes 3 are shielded, the proportion of the silicon carbide particles with different sizes is adjusted, locking bolts 303 are in threaded connection between the turntable rings 301 and the screening inner cylinder 2, the number of the baffle plate 302 corresponds to the group number of the filter holes 3, the baffle plate 302 is arranged between the two adjacent groups of the filter holes 3, and the state of the baffle plate 301 is locked by the locking bolts 303, so that the stability of the baffle plate 302 is effectively improved;|[0046] the screening of different silicon carbide particles is realized by utilizing the filter screen holes 3 with different sizes, as shown in fig. 6, three specifications of filter screen holes 3 are arranged in the drawing, small-sized silicon carbide is screened out by the small-sized filter screen holes 3, small-sized and medium-sized silicon carbide is screened out by the medium-sized filter screen holes 3, small-sized, medium-sized and large-sized silicon carbide is screened out by the large-sized filter screen holes 3, different filter screen holes 3 are shielded by the rotary table ring 301 for rotating the adjusting baffle plate 302, the occupied area of different filter screen holes 3 is changed, and therefore the screening ratio of the particles with different sizes is adjusted, and the mixing effect of the silicon carbide particles is effectively improved.|[0047] 8-9 show that the two ends of the baffle plate 302 are fixedly connected with an extension film 4, one end of the extension film 4 is fixedly connected with a scroll plate 401, the extension film 4 is arranged in a rolling mode by taking the scroll plate 401 as the center, a magnet which is in adsorption connection with the screening inner cylinder 2 is embedded in the scroll plate 401, the extension film 4 is unfolded to realize outward extension of the baffle plate 302, and the shielding effect of the baffle plate 302 on the filter screen hole 3 is effectively improved;|[0048] after the position of the baffle plate 302 is adjusted, the extension film 4 is rolled and unfolded through the scroll plate 401, the shielding area of the baffle plate 302 is extended outwards, the shielding effect on different filter screen holes 3 is effectively improved, and the adhesion effect of the extension film 4 and the screening inner barrel 2 is effectively improved through the adsorption of the scroll plate 401 and the screening inner barrel 2.|[0049] The scope of protection of the above-described embodiments employed in the present application is not limited to the above-described embodiments, and various changes made by those skilled in the art without departing from the spirit of the present application are still within the scope of protection of the present invention. Family Number|(108917837)|108917837|Abstract|(CN117720108 A)|The invention relates to a silicon carbide waste recovery process applied to the technical field of silicon carbide , which comprises the following steps : step 1, firstly , breaking blocky silicon carbide waste into small blocks with fist sizes , and then putting the silicon carbide waste into a crushing mechanism for crushing treatment ; step 2, adjusting and operating crushing equipment to crush the silicon carbide waste into silicon carbide particles with various particle sizes , subsequently mixing the silicon carbide particles with various particle sizes , loading the mixture into a quartz boat , and closing a cover for later use ; and 3, preparing a tube furnace with an air injection hole and an air exhaust hole , introducing high - purity oxygen , putting the quartz boat filled with silicon carbide in the step 2 into the tube furnace , carrying out high - temperature oxidation decarburization , cooling the tube furnace , and taking out the quartz boat to obtain decarburized silicon carbide , so that the silicon carbide waste is crushed into particles with different sizes , and the silicon carbide waste is obtained . And different particles are mixed and put into the quartz boat , so that compared with fine placement of the particles , gaps among the particles are effectively enlarged , and the carbon removal effect of the silicon carbide waste is effectively improved . |IPC codes|(CN117720108 A)|C01B - 032/956 | Environmental technology|Materials, metallurgy B09B-003/35|B09B-003/40|B09B-005/00|C01B-032/956 B09B-003/35|B09B-003/40|B09B-005/00|C01B-032/956 CN120696196 CN120696196 116141356 WHO=Examiner SELF=N CAT=A LAPSED (CN117720108)|LAPSED DEAD (CN117720108)|DEAD (CN117720108)|LEGAL DETAILS FOR CN117720108|Actual or expected expiration date=2025-06-13|Legal state=DEAD|Status=LAPSED|Event publication date=2023-12-18|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202311742439|Application date=2023-12-18|Standardized application number=2023CN-1742439|Event publication date=2024-03-19|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN117720108|Publication stage code=A|Publication date=2024-03-19|Standardized publication number=CN117720108|Event publication date=2024-03-19|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-04-05|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-06-13|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRM/Hd/ijRhgVfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000071817937&ekey=2180&xpn=CN117720108&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=7R65I%252F8xp96vOf7V3F1MjpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN117720108)|CN (CN117720108)|NAME=ZHENGZHOU HENGSHENG TECHNOLOGY Co.,Ltd. , COUNTRY=CN (CN117720108)|NAME=LI ZHIQIANG;Zhengzhou Yichuang Intellectual Property Agency (Special General Partnership) , REG=41138NAME=ZHANG CEN;Zhengzhou Yichuang Intellectual Property Agency (Special General Partnership) , REG=41138 (CN117720108)|NAME=SUN SHAOPENG|NAME=WANG JIFENG|NAME=SHAO BO|NAME=LI LONG|NAME=LIU PENGHAO|NAME=FAN LILI|NAME=XU DENGWAN|NAME=LI XINGYUAN 0 1 Titre: (CN117720108)|Silicon carbide waste recovery process Résumé: (CN117720108)|The invention relates to a silicon carbide waste recovery process applied to the technical field of silicon carbide, which comprises the following steps: step 1, firstly, breaking blocky silicon carbide waste into small blocks with fist sizes, and then putting the silicon carbide waste into a crushing mechanism for crushing treatment; step 2, adjusting and operating crushing equipment to crush the silicon carbide waste into silicon carbide particles with various particle sizes, subsequently mixing the silicon carbide particles with various particle sizes, loading the mixture into a quartz boat, and closing a cover for later use; and 3, preparing a tube furnace with an air injection hole and an air exhaust hole, introducing high-purity oxygen, putting the quartz boat filled with silicon carbide in the step 2 into the tube furnace, carrying out high-temperature oxidation decarburization, cooling the tube furnace, and taking out the quartz boat to obtain decarburized silicon carbide, so that the silicon carbide waste is crushed into particles with different sizes, and the silicon carbide waste is obtained. And different particles are mixed and put into the quartz boat, so that compared with fine placement of the particles, gaps among the particles are effectively enlarged, and the carbon removal effect of the silicon carbide waste is effectively improved. 95 Abstract gpt-4o-mini no The article focuses on a silicon carbide waste recovery process, which does not involve accelerated weathering or CO₂ capture.
95 CN202211552550 CN202211552550 CN115838267 104252674 CN115838267 A 2023-03-24 [CN115838267] 2022-12-05 2022-12-05 2023-03-24 (CN115838267)|2024-11-29 (CN115838267)|Preparation method and application of pervious concrete with pollution reduction and carbon reduction functions (CN115838267)|The invention discloses a preparation method and application of novel pervious concrete with pollution reduction and carbon reduction functions, and belongs to the field of environmental ecological engineering. The preparation method comprises the following steps: firstly, pyrolyzing agricultural waste coconut shells in an oxygen-free environment to obtain crushed coconut shell charcoal, and enabling the coconut shell charcoal to absorb water to be saturated to obtain saturated coconut shell charcoal; the saturated water coconut shell charcoal crushed material is mixed with cement, water and gravel in a certain proportion, then the mixture is put into a mold for standard curing, and the biochar-doped pervious concrete is obtained. The biochar-doped pervious concrete can efficiently purify rainwater runoff pollutants and perform carbon sequestration. According to the invention, resource utilization of agricultural wastes is realized; the biochar-doped pervious concrete which is low in cement consumption, large in specific surface area, rich in porous structure and high in adsorption capacity is prepared; the high-efficiency purification of rainwater runoff is realized; and the goal of assisting carbon neutralization by the carbon sequestration technology is achieved. The biochar-doped pervious concrete has the advantages of being simple to manufacture, low in cost, long in service life, good in water quality purification effect and the like. BEIJING UNIVERSITY OF CIVIL ENGINEERING & ARCHITECTURE (CN115838267)|Beijing University of Civil Engineering and Architecture ([CN]) ZHANG ZIYANG|PENG XINYU|ZHANG XIAOXIAN|LI FEI|CHEN HONGRUI|ZHANG XIAORAN|TAN CHAOHONG|LI HAIYAN (CN115838267)|ZHANG ZIYANG|PENG XINYU|ZHANG XIAOXIAN|LI FEI|CHEN HONGRUI|ZHANG XIAORAN|TAN CHAOHONG|LI HAIYAN (CN115838267)|MINGLIANG XIN;BEIJING PROFESSIONAL INTELLECTUAL PROPERTY AGENCY LTD|Reg. Nb: 11944 (CN115838267)|Compared with the prior art, the preparation method and the application of the pervious concrete with the functions of reducing pollution and carbon have the following advantages:|Compared with the prior sealing and storing technology, the method has the advantages that the coconut shell carbon is sealed and stored in the pervious concrete, the operation is simple, and the carbon sealing and storing can be effectively realized. Coconut charcoal is a very good CO due to its affinity for non-polar compounds and high proportion of surface pores 2 The adsorbent has good advantages for isolating carbon in pervious concrete;|and sixthly, the method for treating runoff pollutants by using the pervious concrete with the functions of reducing pollution and carbon has the advantages of good adsorption performance, high pollutant treatment efficiency and the like, and is a widely adopted method for treating runoff pollution of rainwater.| (CN115838267)|1. The preparation method of the pervious concrete with the functions of reducing pollution and carbon is characterized by comprising the following steps:pyrolyzing and carbonizing coconut shells in an anoxic environment to obtain coconut shell carbon;enabling the coconut shell carbon to absorb water and saturate to obtain saturated water coconut shell carbon; andstirring the saturated water coconut shell carbon, cement, broken stone, water and a high-efficiency water reducing agent according to a certain mass ratio, wherein the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 5 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent.| (CN115838267)|Referring to fig. 1, the present invention provides a method for preparing a pervious concrete with pollution-reducing and carbon-reducing functions, that is, a method for preparing a coconut shell carbon-doped pervious concrete, comprising the following steps:|The invention discloses a preparation method and application of novel pervious concrete with functions of reducing pollution and carbon, and belongs to the field of environmental ecological engineering.|Therefore, the construction method is a feasible road for constructing the sponge city with low carbon, reducing the whole carbon footprint of the pervious concrete, and improving the carbon fixing capacity and decontamination effect of the pervious concrete. Disclosure of Invention In view of the above, the invention provides a preparation method and application of a novel pervious concrete with pollution-reducing and carbon-reducing functions for reducing the overall carbon footprint of the pervious concrete, improving the carbon fixing capacity and the decontamination and purification effects of the pervious concrete.| (CN115838267)|PERVIOUS CONCRETE(100,97)|CARBON(100,26)|POLLUTION REDUCTION(100,26)|POLLUTION REDUCTION FUNCTION(100,21)|CARBON REDUCING FUNCTION(100,8)|POLLUTION REDUCING FUNCTION(100,8)|RAINWATER TREATING RUNOFF POLLUTION(84,2)|COCONUT SHELL CARBON(82,138)|BROKEN ROCK(80,47)|BIOCHAR DOPED PERVIOUS CONCRETE(75,3)|RAINWATER POLLUTION PURIFICATION(63,1)|RAINWATER RUNOFF POLLUTANT(59,1)|COCONUT SHELL CHARCOAL(57,24)|TREATING RUNOFF POLLUTANT(56,3)|TREATING RUNOFF POLLUTION(56,2)|ANOXIC ENVIRONMENT(52,9)|FEASIBLE ROAD(47,1)|CEMENT(46,44)|DECONTAMINATION(46,2)|TREATING RUNOFF CONTAMINANT(45,2)|PYROLYZING AGRICULTURAL WASTE(45,1)|COCONUT SHELL(41,50)|SATURATED COCONUT SHELL CARBON(41,27)|CEMENT CONSUMPTION(41,1)|NONPOLAR COMPOUND(41,1)|WATER COCONUT SHELL CARBON(39,32)|POLLUTANT TREATMENT(38,2)|CARBON FOOTPRINT(37,4)|CARBON NEUTRALIZATION TARGET(37,1)|RAIN WATER POLLUTION(35,3)|ANAEROBIC ENVIRONMENT(35,1)|SPONGE CITY(34,6)|RESOURCE UTILIZATION(33,2)|ADSORPTION CAPACITY(33,1)|ISOLATING CARBON(33,1)|CARBON FIXING CAPACITY(31,2)|ECOLOGICAL ENGINEERING(31,2)|ADSORPTION PERFORMANCE(30,2)|ADSORBENT(29,1)|COCONUT CHARCOAL(27,1)|CARBON SEQUESTRATION(25,2)|VENTILATED ENVIRONMENT(24,3)|CARBON SEALING(23,2)|CARBON DOPED PERVIOUS CONCRETE(22,20)|COOL ENVIRONMENT(21,3)|STANDARD MAINTENANCE(21,1)|CONCRETE PERMEABILITY(20,8)|AGGREGATE(20,1)|WATER ABSORBING(19,3)|RICH PORE STRUCTURE(18,1)|REDUCING AGENT(17,38)|SATURATED WATER COCONUT SHELL(17,4)|PURIFICATION(16,5)|MASS RATIO(15,24)|CRUSHED STONE(15,7)|DEMOLDING(15,3)|STANDARD CURING ROOM(15,3)|ECOLOGICAL ENGINEERING FIELD(15,2)|PERVIOUS CONCRETE SLURRY PHOTOGRAPH(15,2)|LONG SERVICE LIFE(15,1)|ARTIFICAL RAINWATER SIMULATION(14,1)|RAINWATER RUNOFF POLLUTION(13,2)|REDUCING RUNOFF POLLUTION(12,3)|PRIOR SEALING(11,1)|WATER PERMEABILITY COEFFICIENT(10,5)|BALL MILL(10,4)|AIR DRYING TREATMENT(10,3)|PORE SURFACE(10,2)|SIMULATED RUNOFF(10,2)|WATER PURIFICATION(10,1)|AIR DRIED COCONUT SHELL(9,4)|COMPREHENSIVE GREEN TRANSFORMATION(9,1)|GOLDEN CORNER BRAND(9,1)|PERVIOUS PAVING(9,1)|PYROLYSIS CARBONIZATION(9,1)|PYROLYTIC CARBONIZATION(9,1)|RAINFALL SIMULATION(9,1)|SAMPLING PORT(8,3)|CARBON DOPED PERMEABLE CONCRETE(8,2)|CHARCOAL DOPED PERVIOUS CONCRETE(8,2)|BIOMASS FEEDSTOCK(8,1)|COCONUT HUSK CHARCOAL(8,1)|RAINFALL FLOOD MANAGEMENT CONCEPT(8,1)|RAINWATER RUNOFF ABSORPTION(8,1)|SATURATED COCONUT SHELL CHARCOAL(8,1)|OXYGEN DEFICIENT ENVIRONMENT(7,3)|CARBON PERMEABLE CONCRETE(7,1)|COCONUT SHELL PHOTOGRAPH(7,1)|COCONUT SHELL PULVERIZATION(7,1)|CONTAMINATION PROMOTION(7,1)|DIRT CLEANING CAPABILITY(7,1)|DOPING PROPORTION(7,1)|ECONOMIC SOCIETY DEVELOPMENT(7,1)|PAVING TOTAL INFLOW(7,1)|RAINWATER FLOOD MANAGEMENT(7,1)|REDUCING RUNOFF RAINWATER(7,1)|ROBBING MOISTURE(7,1)|RUNOFF POLLUTION LOAD(7,1)|URBANIZATION RAPID DEVELOPMENT(7,1)|PERMEABLE PAVEMENT(6,3)|AMMONIA NITROGEN(6,2)|NITRATE NITROGEN(6,2)|SHAKING MACHINE(6,2)|INERT GAS(5,4)|CURING PERIOD(5,2)|FLOW CONTAMINATION(5,2)|HYDRATION PRODUCT(5,2)|PERVIOUS CONCRETE LAYER(5,2)|UNDERLAYER(5,2)|WATER PERMEABLE PAVING(5,2)|AGRICULTURAL WASTE COCONUT SHELL(5,1)|ARGON PURGE(5,1)|CEMENT PARTICLE(5,1)|COCONUT SHELL CARBON PHOTOGRAPH(5,1)|COCONUT SHELL MOISTURE CONTENT(5,1)|CONCRETE STIRRING EQUIPMENT(5,1)|DOPING COCONUT SHELL CARBON(5,1)|ECOLOGICAL BENEFIT(5,1)|ECOLOGICAL ENVIRONMENT(5,1)|PERVIOUS CONCRETE BRITTLE FAILURE(5,1)|QUARTZ BOAT(5,1)|TARGET POLLUTANT(5,1)|CARBON DIOXIDE(4,4)|CRUSHED MATERIAL(4,3)|SAMPLE CONNECTION(4,3)|GRAVEL(4,2)|ADDED PERMEABLE CONCRETE(4,1)|ANAEROBIC CONDITION(4,1)|CARBON RICH SIEVED SUBSTANCE(4,1)|COCONUT COMPRESSIVE STRENGTH(4,1)|COCONUT SHELL CARBON POWDER(4,1)|CRUSHING TREATMENT(4,1)|CURING AGE(4,1)|ECOLOGICAL CIVILIZATION(4,1)|ENHANCING CITY WATER(4,1)|MICROFILLER(4,1)|ORDINARY PORTLAND CEMENT(4,1)|PERCENTAGE CONTENT(4,1)|PERMANENT SEALING(4,1)|PERVIOUS CONCRETE BASIC PERFORMANCE(4,1)|PERVIOUS CONCRETE CARBON EMISSION(4,1)|PERVIOUS CONCRETE COMPRESSIVE STRENGTH(4,1)|POLYCARBOXYLATE WATER REDUCER(4,1)|PREVENTION CAPACITY(4,1)|PURIFICATION CAPACITY(4,1)|REMOVING POLLUTANT(4,1)|SHRINKAGE RESISTANCE(4,1)|SOIL MATRIX(4,1)|SUPERSATURATED WATER(4,1)|TEST ITEM(4,1)| (CN115838267)|1. The preparation method of the pervious concrete with the functions of reducing pollution and carbon is characterized by comprising the following steps:|pyrolyzing and carbonizing coconut shells in an anoxic environment to obtain coconut shell carbon;|enabling the coconut shell carbon to absorb water and saturate to obtain saturated water coconut shell carbon; and|stirring the saturated water coconut shell carbon, cement, broken stone, water and a high-efficiency water reducing agent according to a certain mass ratio, wherein the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 5 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent.|2. The method for preparing pervious concrete with pollution-reducing and carbon-reducing functions as claimed in claim 1, wherein before the coconut shell is pyrolyzed and carbonized in an anoxic environment, the coconut shell is placed in a cool and ventilated environment for air drying treatment to reduce the moisture of the coconut shell to below 20%, and then the air-dried coconut shell is pulverized to obtain a pulverized material with the length of 2cm to 3 cm.|3. The method for preparing pervious concrete with pollution-reducing and carbon-reducing functions as claimed in claim 2, wherein before the coconut shell charcoal is saturated with water, the coconut shell charcoal is put into a ball mill to be crushed for 30min and then is sieved through a 200-mesh sieve to obtain coconut shell charcoal powder.|4. The method for preparing pervious concrete with pollution-reducing and carbon-reducing functions as claimed in claim 1, wherein the anoxic environment is formed by introducing inert gas or vacuumizing; and/or|The temperature for pyrolyzing and carbonizing the coconut shells is 500-750 ℃; and/or|Heating to 500-750 deg.C at a rate of 10 deg.C/min, and standing at 500-750 deg.C for 0.5-8 h.|5. The method for preparing pervious concrete with pollution-reducing and carbon-reducing functions as claimed in claim 1, wherein the method for preparing saturated coconut shell carbon comprises the following steps:|adding 1 part of coconut shell carbon into 2 parts of water, and stirring for 60-90 s;|and adding 1 part of water, and stirring for 15-30 s until the mixture is pasty to obtain the saturated coconut shell carbon.|6. The method for preparing pervious concrete with pollution-reducing and carbon-reducing functions as claimed in claim 1, wherein the mass ratio of coconut shell carbon, cement, broken stone, water and high efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 25 parts of coconut shell carbon, 1000 parts of cement, 3500 parts of broken stone, 300 parts of water and 7.5 parts of a high-efficiency water reducing agent in the saturated water coconut shell carbon; or 25 parts of coconut shell carbon, 1000 parts of cement, 3500 parts of broken stone, 280 parts of water and 7.5 parts of a high-efficiency water reducing agent in the saturated water coconut shell carbon.|7. The method for preparing pervious concrete with pollution-reducing and carbon-reducing functions as claimed in claim 1, wherein the mass ratio of water to cement is 1:2 to 1:5.|8. the method for preparing the pervious concrete with the functions of reducing pollution and carbon according to claim 1, wherein the process of stirring the saturated coconut shell carbon, the cement, the broken stone, the water and the high efficiency water reducing agent according to a certain mass ratio comprises the following steps:|firstly, adding all the broken stones into a concrete stirring device, stirring for 15s to 30s, then adding 1/2 of water, and stirring for 30s to 60s;|adding all the cement and the rest 1/2 of the water, and continuously stirring for 30-60 s;|and finally, adding the saturated coconut shell carbon, and stirring for 60 to 90 seconds until the mixture reaches a flowing state to obtain the pervious concrete with the functions of reducing pollution and carbon.|9. The method for preparing the pervious concrete with the functions of reducing pollution and carbon according to claim 1, wherein after the saturated coconut shell carbon, the cement, the broken stone, the water and the high efficiency water reducing agent are stirred according to a certain mass ratio, the method further comprises the following steps:|die filling and forming; and|and demolding, and carrying out standard curing in a standard curing room for a period of time.|10. A method of treating runoff contaminants comprising the steps of:|providing the pervious concrete with pollution-reducing and carbon-reducing functions as claimed in any one of claims 1 to 9; and|the pervious concrete with the functions of reducing pollution and carbon is applied to sponge city construction to realize the purification of rainwater pollution. (CN115838267)|TECHNICAL FIELD|[0001] The invention belongs to the field of environmental ecological engineering, and particularly relates to a preparation method and application of novel pervious concrete with functions of reducing pollution and carbon.|BACKGROUND ART|[0002] As a new generation of urban rainfall flood management concept, the sponge city is newly built with various rainwater and accumulated water absorption, purification and dredging facilities, so that the city has toughness and elasticity like sponge, and has positive effects on repairing city water ecology, conserving water resources, enhancing city waterlogging prevention capacity and reducing runoff pollution. The ecological civilization construction of China enters the key period of taking carbon reduction as a key strategic direction, promoting pollution and carbon reduction synergistic interaction, promoting the development of economic society and comprehensive green transformation and realizing the quality improvement of ecological environment from quantitative change to qualitative change. Therefore, how to construct sponge cities on the basis of low carbon is the key point of low carbon ecological construction.|[0003] With the rapid development of urbanization, rainwater runoff has developed into a main factor of urban non-point source pollution. The pervious concrete is one of main technical measures of 'seepage' in sponge city construction, can effectively reduce runoff pollution load, and achieves the effects of purifying water quality and improving urban water environment. However, the carbon emission of the pervious concrete in the production and transportation process is not negligible. Therefore, the construction method is a feasible road for constructing the sponge city with low carbon, reducing the whole carbon footprint of the pervious concrete, and improving the carbon fixing capacity and decontamination effect of the pervious concrete.|DISCLOSURE|Disclosure of Invention|[0004] In view of the above, the invention provides a preparation method and application of a novel pervious concrete with pollution-reducing and carbon-reducing functions for reducing the overall carbon footprint of the pervious concrete, improving the carbon fixing capacity and the decontamination and purification effects of the pervious concrete. In the preparation method and application of the novel pervious concrete with pollution-reducing and carbon-reducing functions, the coconut shell carbon is sealed in the pervious concrete, so that carbon sealing is realized, and the effect of reducing carbon is achieved; meanwhile, the prepared coconut shell carbon-doped pervious concrete has a porous structure, is beneficial to adsorbing and removing pollutants, and can realize a purification function on rainwater runoff pollution by applying the coconut shell carbon-doped pervious concrete to sponge city construction, so that pollution reduction and carbon reduction synergistic effect is realized.|[0005] A preparation method of pervious concrete with pollution-reducing and carbon-reducing functions comprises the following steps: pyrolyzing and carbonizing coconut shells in an anoxic environment to obtain coconut shell carbon; enabling the coconut shell carbon to absorb water and saturate to obtain saturated water coconut shell carbon; and stirring the saturated water coconut shell carbon, cement, gravel, water and a high-efficiency water reducing agent according to a certain mass ratio, wherein the mass ratio of the coconut shell carbon, the cement, the gravel, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 5 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent.|[0006] Further, before pyrolyzing and carbonizing the coconut shells in an anoxic environment, the coconut shells are placed in a cool and ventilated environment for air drying treatment, so that the moisture of the coconut shells is reduced to be below 20%, and then the air-dried coconut shells are crushed to obtain crushed materials with the length of 2 cm-3 cm.|[0007] Further, the oxygen-deficient environment is formed by introducing inert gas or vacuumizing; and/or, the temperature for pyrolyzing and carbonizing the coconut shell is 500-750 ℃; and/or increasing the temperature to 500-750 ℃ at a rate of 10 ℃/min and staying at 500-750 ℃ for 0.5-8 h.|[0008] Further, before the coconut shell charcoal is saturated by absorbing water, the coconut shell charcoal is put into a ball mill to be crushed for 30min and then passes through a 200-mesh screen to obtain coconut shell charcoal powder.|[0009] Further, the preparation method of the saturated coconut shell carbon comprises the following steps: adding 1 part of coconut shell carbon into 2 parts of water, and stirring for 60-90 s; and adding 1 part of water, and stirring for 15-30 s until the mixture is pasty to obtain the saturated coconut shell carbon.|[0010] Further, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 25 parts of coconut shell carbon, 1000 parts of cement, 3500 parts of broken stone, 300 parts of water and 7.5 parts of a high-efficiency water reducing agent in the saturated water coconut shell carbon; or 25 parts of coconut shell carbon, 1000 parts of cement, 3500 parts of broken stone, 280 parts of water and 7.5 parts of a high-efficiency water reducing agent in the saturated water coconut shell carbon.|[0011] Further, the mass ratio of the water to the cement is 1:2 to 1:5.|[0012] further, the process of stirring the saturated coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent according to a certain mass ratio comprises the following steps: firstly, adding all the broken stones into a concrete stirring device, stirring for 15s to 30s, then adding 1/2 of water, and stirring for 30s to 60s; adding all cement and the rest 1/2 of water, and continuously stirring for 30-60 s; and finally, adding the saturated coconut shell carbon, and stirring for 60 to 90 seconds until the mixture reaches a flowing state to obtain the pervious concrete with the functions of reducing pollution and carbon.|[0013] Further, after the saturated coconut shell carbon, cement, broken stone, water and the high-efficiency water reducing agent are stirred according to a certain mass ratio, the method comprises the following steps: die filling and forming; and demolding, and carrying out standard curing in a standard curing room for a period of time.|[0014] A method of treating runoff contaminants comprising the steps of: providing the pervious concrete with the functions of reducing pollution and carbon; and applying the pervious concrete with the functions of reducing pollution and carbon in sponge city construction to purify rainwater pollution.|[0015] Compared with the prior art, the preparation method and the application of the pervious concrete with the functions of reducing pollution and carbon have the following advantages:|[0016] firstly, the coconut shell carbon is doped or sealed in the pervious concrete, so that the agricultural solid waste recovery can be effectively promoted, the utilization rate of agricultural wastes can be effectively improved, andthe carbon fixation capacity and the possibility of greatly reducing the land area required by waste disposal are achieved, and the ecological benefit is very obvious. Meanwhile, the coconut shell charcoal can reduce about 870 kilograms of CO per ton of dry raw material according to the type of the raw material and the preparation conditions 2 Equivalent net greenhouse gas emissions, with 62% to 66% being achieved by carbon capture and storage of biomass feedstock of coconut shell char. Compared with the prior sealing and storing technology, the method has the advantages that the coconut shell carbon is sealed and stored in the pervious concrete, the operation is simple, and the carbon sealing and storing can be effectively realized. Coconut charcoal is a very good CO due to its affinity for non-polar compounds and high proportion of surface pores 2 The adsorbent has good advantages for isolating carbon in pervious concrete;|[0017] secondly, the coconut shell carbon has the characteristic of surface roughness, can promote the adhesion of the coconut shell carbon and pervious concrete slurry, has the capacity of building a bridge between micropores on an interface transition area and hydration products, and is beneficial to redistribution of stress. Therefore, the coconut shell charcoal can avoid the brittle failure of pervious concrete. In addition, the water absorption and retention performance of the coconut shell carbon can improve the water evaporation and shrinkage resistance of the pervious concrete slurry, and meanwhile, the moisture contained in the coconut shell carbon can promote the hydration process of the pervious concrete, so that the compressive strength of the pervious concrete is improved. The coconut shell carbon is doped into the pervious concrete, so that the basic performance of the pervious concrete can be effectively enhanced. In addition, pervious concrete is used as a common material in sponge city construction, and is mostly used for absorbing rainwater runoff and reducing runoff pollution. The permeable concrete doped with coconut shell carbon can further improve the dirt cleaning capability of the permeable concrete, thereby realizing the dual functions of carbon fixation and pollution reduction. Therefore, the coconut shell carbon doped pervious concrete has the functions of reducing pollution and carbon;|[0018] thirdly, coconut shell charcoal is a carbonaceous material which takes agricultural wastes as raw materials and can be produced by various processes. The coconut shell carbon is partially doped into the concrete, so that the micro-filler and the internal curing effect can be exerted, the mechanical property and the durability of the concrete are improved, the stable carbon element is stored in the concrete, and the permanent sealing can be realized, so that the aim of reducing carbon is fulfilled;|[0019] and fourthly, the coconut shell carbon is used as an efficient environment adsorption material, multiple adsorption and purification mechanisms are provided for target pollutants, the rainwater runoff pollution purification capacity of the coconut shell carbon can be further enhanced, and important help is provided for coordinating rainwater flood management, reducing runoff pollution and constructing a low-carbon sponge city. Therefore, the coconut shell carbon is added into the pervious concrete, so that the system effect can be exerted to the maximum extent, the resource utilization and carbon source recycling of agricultural wastes are realized, the requirements of pollution reduction and carbon reduction are met, and the coconut shell carbon permeable concrete has extremely high application value and practical significance;|[0020] fifthly, the coconut shell carbon doped pervious concrete has low preparation cost and high performance;|[0021] and sixthly, the method for treating runoff pollutants by using the pervious concrete with the functions of reducing pollution and carbon has the advantages of good adsorption performance, high pollutant treatment efficiency and the like, and is a widely adopted method for treating runoff pollution of rainwater.|DRAWINGS DESCRIPTION|[0022] FIG. 1 is a flow chart of a preparation method of pervious concrete with pollution-reducing and carbon-reducing functions provided by the invention.|[0023] FIG. 2 is a flow chart of the method for preparing coconut shell charcoal from agricultural wastes provided by the invention.|[0024] FIG. 3 is a Scanning Electron Microscope (SEM) photograph of coconut shell carbon provided by the present invention.|[0025] FIG. 4 is an SEM photograph of a pervious concrete slurry provided by the present invention after doping with coconut shell carbon.|[0026] Fig. 5 is a schematic structural diagram of the water permeable paving device for simulating the effect of removing pollutants according to the present invention.|[0027] FIG. 6 is a coconut shell carbon-doped pervious concrete facing pair with different coconut shell carbon addition amounts according to the present invention(Ammonia nitrogen) removal effect.|[0028] FIG. 7 shows the effect of coconut shell carbon doped pervious concrete surface layer on COD (chemical oxygen demand) removal at different coconut shell carbon addition levels.|[0029] FIG. 8 shows the TN (total nitrogen) removal effect of the coconut shell carbon-doped pervious concrete surface layer provided by the present invention at different coconut shell carbon addition levels.|[0030] FIG. 9 shows the TP (total phosphorus) removal effect of the coconut shell carbon-doped pervious concrete surface layer under different coconut shell carbon addition amounts.|[0031] FIG. 10 shows the NO ratio of the coconut shell carbon-doped pervious concrete surface course under different coconut shell carbon addition amounts 3 The effect of removing N (nitrate nitrogen).|[0032] FIG. 11 shows the effect of removing Cu (copper) from the coconut shell carbon doped pervious concrete surface layer at different addition levels of coconut shell carbon.|[0033] FIG. 12 shows the effect of removing heavy Pb (lead) from the coconut shell carbon-doped pervious concrete surface layer at different amounts of coconut shell carbon.|[0034] FIG. 13 shows the effect of removing heavy Zn (Zn) from the coconut shell carbon doped pervious concrete surface layer at different addition amounts of coconut shell carbon.|[0035] Description of the main reference numerals:|[0036] 10-a pervious concrete layer; 20-a base layer; 30-an underlayer; 40-soil base; 1-a sampling port; 2-a sampling port; 3-a sampling port; 4-sampling port.|INVENTION MODE|Detailed Description|[0037] The technical solution of the present invention will be described below by way of specific examples. It is to be understood that one or more of the steps referred to in the present application do not exclude the presence of other methods or steps before or after the combination of steps, or that other methods or steps may be intervening between those steps specifically referred to. It should also be understood that these examples are intended only to illustrate the invention and are not intended to limit the scope of the invention. Unless otherwise indicated, the numbering of the method steps is only for the purpose of identifying the method steps, and is not intended to limit the arrangement order of each method or the scope of the implementation of the present invention, and changes or modifications of the relative relationship thereof may be regarded as the scope of the implementation of the present invention without substantial technical change.|[0038] The preparation method and application of the pervious concrete with pollution-reducing and carbon-reducing functions provided by the invention are further explained in the following by combining the attached drawings.|[0039] Referring to fig. 1, the present invention provides a method for preparing a pervious concrete with pollution-reducing and carbon-reducing functions, that is, a method for preparing a coconut shell carbon-doped pervious concrete, comprising the following steps:|[0040] s1, pyrolyzing and carbonizing coconut shells in an anoxic environment to obtain coconut shell carbon; and|[0041] and S2, stirring the coconut shell carbon, cement, broken stone, water and a high-efficiency water reducing agent according to a certain mass ratio to obtain the coconut shell carbon-doped pervious concrete, wherein the coconut shell carbon-doped pervious concrete is the pervious concrete with the functions of reducing pollution and carbon.|[0042] In step S1, preferably, the coconut shell is air-dried before the pyrolysis carbonization, so that the moisture of the coconut shell is reduced to less than 20%. Preferably, the air-dried coconut shell is subjected to mixing and crushing treatment by using a method such as manual crushing, mechanical crushing and the like to obtain crushed material with the length of 2cm (centimeter) to 3 cm.|[0043] In the step S2, the coconut shell is pyrolyzed and carbonized at high temperature in an anoxic environment or an anoxic environment to prepare the coconut shell carbon. Since the coconut shell charcoal is prepared from agricultural waste, the coconut shell charcoal is also referred to as agricultural waste-based coconut shell charcoal. Due to anoxic environment, the agricultural waste is blocked from being converted into carbon dioxide (CO) 2 )。|[0044] In one embodiment, the air-dried and pulverized coconut shells are placed in a quartz boat and placed in a tube furnace for pyrolytic carbonization.|[0045] The oxygen-deficient environment can be formed by introducing inert gas or vacuumizing, and the inert gas comprises argon and the like. In one embodiment, the oxygen deficient environment is formed using an argon purge.|[0046] The temperature for pyrolyzing and carbonizing the coconut shells is 500 ℃ to 750 ℃. In one embodiment, the temperature in the tube furnace is increased to 500 ℃ to 750 ℃ at a rate of 10 ℃/min (degrees/min) and is maintained at 500 ℃ to 750 ℃ for a period of time, i.e., a carbonization time for pyrolytically carbonizing the coconut shell, which is 0.5h (hours) to 8h.|[0047] And the step S2 further comprises the step of crushing and sieving the coconut shell charcoal to obtain coconut shell charcoal powder. Specifically, after the coconut shell charcoal is cooled, the coconut shell charcoal is crushed and sieved to obtain coconut shell charcoal powder, namely agricultural waste-based coconut shell charcoal powder. In one embodiment, the coconut shell charcoal is pulverized by a ball mill, and is sieved by a 40-200 mesh sieve, and after shaking by a shaking machine, a carbon-rich sieved substance is collected, and the sieved substance is the coconut shell charcoal powder.|[0048] And the step S2 further comprises the step of enabling the coconut shell carbon to absorb water and saturate to obtain saturated water coconut shell carbon. That is, it is preferable that before the step S3 "mixing the coconut shell charcoal, the cement, the crushed stone, the water and the high efficiency water reducing agent according to a certain mass ratio" is performed, the coconut shell charcoal is saturated by absorbing water in advance, so as to avoid the coconut shell charcoal from robbing moisture necessary for the hydration of the concrete, and the moisture stored in the saturated coconut shell charcoal can further promote the hydration reaction of the concrete.|[0049] In a specific embodiment, the preparation method of the saturated coconut shell carbon comprises the following steps: adding 1 part of coconut shell carbon into 2 parts of water, and stirring for 60s (seconds) to 90s; and adding 1 part of water, and stirring for 15-30 s until the mixture is pasty, wherein the obtained product is the saturated coconut shell carbon.|[0050] In the step S2, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent is as follows: 0 to 50 parts of coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent. In a specific embodiment, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent is as follows: 0 to 50 parts of coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 5 to 10 parts of high-efficiency water reducing agent. In a specific embodiment, the coconut shell carbon absorbs water to be saturated to become saturated water coconut shell carbon, and the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 0 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent. In a specific embodiment, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 0 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 5 to 10 parts of high-efficiency water reducing agent. Preferably, the coconut shell carbon in the saturated coconut shell carbon can be 5 parts, 6.25 parts, 10 parts, 12.5 parts, 15 parts, 20 parts, 30 parts, 40 parts or 50 parts. In a specific embodiment, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 5 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent.|[0051] The mass ratio of the water to the cement (namely the water cement ratio) is 1:2 to 1:5. the types of the cement, the broken stone and the high-efficiency water reducing agent are not limited. In a specific embodiment, the cement is P.O42.5 type portland cement, the crushed stone is made of basalt, the particle size of the crushed stone is 4.75mm (millimeters) to 9.5mm, the high-efficiency water reducing agent is a polycarboxylic acid water reducing agent, and the water reducing rate of the polycarboxylic acid water reducing agent is not less than 20%.|[0052] In a specific embodiment, the saturated water coconut shell carbon, the cement, the broken stone, the water and the high efficiency water reducing agent are weighed according to a certain mass ratio and placed into a concrete stirring device until the materials are uniformly stirred, so that the novel permeable concrete with the functions of reducing pollution and carbon and having low cost and high performance is prepared.|[0053] In a specific embodiment, the process of stirring the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent according to a certain mass ratio is as follows: firstly, adding all the broken stones into the concrete stirring equipment, stirring for 15s to 30s, then adding 1/2 of water, and stirring for 30s to 60s; adding all the cement and the rest 1/2 of the water, and continuously stirring for 30-60 s; and finally, adding saturated coconut shell carbon, and stirring for 60 to 90 seconds until the mixture reaches a flowing state, thereby obtaining the pervious concrete with the functions of reducing pollution and carbon.|[0054] Further, as shown in fig. 1, after the step S2 "mixing the coconut shell charcoal, the cement, the crushed stone, the water and the high efficiency water reducing agent according to a certain mass ratio", the method for preparing the pervious concrete with the functions of reducing pollution and carbon may further include the following steps:|[0055] s3, stirring the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent according to a certain mass ratio to obtain a mixture, continuously stirring the mixture, and filling and molding the mixture; and|[0056] and S4, demolding, and carrying out standard curing in a standard curing room for a period of time.|[0057] In step S3, in one embodiment, the mixer continuously mixes the mix for 2 minutes and 30 seconds.|[0058] In step S4, in a specific embodiment, standard curing is performed for 28 days to obtain the novel coconut shell carbon-doped permeable concrete with the functions of reducing pollution and carbon.|[0059] The concrete examples of the preparation method of the pervious concrete with the functions of reducing pollution and carbon are as follows.|[0060] Detailed description of the preferred embodiment 1|[0061] FIG. 2 is a flow chart of the process of preparing coconut shell charcoal from the agricultural wastes. In this embodiment, the agricultural waste is coconut shells, and the coconut shells are placed in a cool and ventilated environment for air-drying treatment, so that the moisture content of the coconut shells is reduced to below 20%. And then mechanically crushing the air-dried coconut shells by a crusher to obtain crushed materials with the length of 2cm to 3 cm. Then, the crushed material is placed in a tube furnace, argon is introduced to produce an anaerobic condition, the temperature is raised to 500 ℃ at the speed of 10 ℃/min, and the black carbon-shaped object, namely the coconut shell biochar, is obtained after pyrolysis and carbonization for 30 min. And after cooling, putting the coconut shell biochar into a ball mill for crushing for 30min, then sieving the coconut shell biochar through a 200-mesh sieve, and collecting sieved substances after shaking by a shaking machine to obtain coconut shell carbon powder. Table 1 lists the basic chemical compositions of coconut shell carbon. From table 1, the percentage contents of five elements, phosphorus (P), oxygen (O), silicon (Si), carbon (C), and chlorine (Cl), were found, wherein carbon (C) was 83.7%. Thus, it can be seen from Table 1 that the coconut shell carbon is rich in carbon, which indicates that the coconut shell carbon is a carbon-rich material and that the coconut shell carbon can be effectively fixed by doping the coconut shell carbon into pervious concrete. FIG. 2 is an SEM photograph of coconut shell biochar, and it can be observed from FIG. 2 that the surface pore structure of the coconut shell carbon is more developed, and the specific surface area of the coconut shell carbon is increased, so that the coconut shell carbon is in wider contact with pollutants on one hand, and is more favorable for adsorbing the pollutants; on the other hand, the coconut shell carbon can store more water, is beneficial to the adhesion of cement particles and the coconut shell carbon, and further promotes the hydration reaction of concrete, thereby increasing the hydration products.|[0062] TABLE 1 basic chemical composition of coconut husk charcoal|[0063] Density (g/cm) 3 )P(%)O(%)Si(%)C(%)Cl(%)pH1.473.411.21.383.70.37.59|[0064] Specific example 2|[0065] In this example, the water-cement ratio was designed to be 1: and 3, weighing 1000 parts of cement, 300 parts of water, 3500 parts of broken stone, 0 to 50 parts of coconut shell carbon in the saturated coconut shell carbon and 7.5 parts of high-efficiency water reducing agent according to the mass mixing ratio.|[0066] In the embodiment, the water meets the three types of water quality standards of the surface or better than the three types of water quality standards specified by the national standard GB3838-2002, the cement adopts the golden corner brand P.O42.5 grade ordinary portland cement, and the polycarboxylate water reducer is purchased from the Fine chemical industry Co., ltd.|[0067] In the embodiment, all the crushed stones are added into concrete stirring equipment to be stirred for 15s to 30s, then 150 parts of water is added, and the mixture is stirred for 30s to 60s; adding all cement and 150 parts of water, and continuously stirring for 30-60 s; and finally, adding saturated water coconut shell carbon, wherein the parts of the coconut shell carbon in the saturated water coconut shell carbon are respectively 0, 6.25, 12.5, 25 and 50, stirring for 60-90 s until the mixture reaches a flowing state, and thus obtaining the novel permeable concrete with pollution-reducing and carbon-reducing functions in different doping proportions of the coconut shell carbon. Fig. 4 is an SEM photograph of the pervious concrete slurry provided by the present invention after doping coconut shell carbon. From the microstructure shown in fig. 4, it can be seen that the coconut shell carbon is embedded in the concrete slurry, indicating that the coconut shell carbon doped pervious concrete is successfully prepared.|[0068] The compressive strength and the water permeability coefficient of the pervious concrete are the most basic and important test items in a plurality of performance indexes of the pervious concrete, and the compressive strength and the water permeability coefficient of the prepared test block (namely the saturated coconut shell carbon-doped pervious concrete) are measured according to a test method specified by JC/T2558-2020 permeable concrete. The compressive strength and the water permeability coefficient of the pervious concrete under different addition amounts of the coconut shell carbon and the saturated water coconut shell carbon are respectively shown in the table 2 and the table 3, wherein the reference sample coconut shell carbon is not treated by supersaturated water. It can be seen from table 2 that, as the curing period increases, the compressive strength of the concrete continuously increases with the increase of the content of the saturated water coconut shell carbon in the concrete doped with five different proportions of the saturated water coconut shell carbon, that is, in the same curing period, the compressive strength of the concrete can be obviously increased by doping the saturated water coconut shell carbon, and when the doping amount of the saturated water coconut shell carbon is 25 parts, the compressive strength of the concrete reaches the strongest level. The coconut shell carbon doped with unsaturated water can enhance the compressive strength of concrete in a short term, but reduces the compressive strength of concrete in a long term. Therefore, the saturated coconut shell carbon is more feasible to select. Table 3 shows that the addition of saturated coconut shell carbon does not significantly change the permeability coefficient of concrete, demonstrating its potential in reducing runoff rain.|[0069] TABLE 2 compressive Strength of coconut carbon-doped pervious concrete and saturated coconut carbon-doped pervious concrete|[0070] |[0071] TABLE 3 Permeability coefficient of saturated coconut shell carbon-doped pervious concrete|[0072] |[0073] |[0074] Specific example 3|[0075] In this example, the water-cement ratio is designed to be 1:2.8, weighing 1000 parts of cement, 280 parts of water, 3500 parts of broken stone, 0 to 50 parts of coconut shell carbon in the saturated coconut shell carbon and 7.5 parts of high-efficiency water reducing agent according to the mass mixing ratio. The specific materials and methods were the same as in example 2.|[0076] And (3) according to a test method specified by JC/T2558-2020 pervious concrete, measuring the compressive strength and the water permeability coefficient of the prepared test block (namely the saturated coconut shell carbon doped pervious concrete). Tables 4 and 5 show the compressive strength and water permeability coefficient of the saturated coconut shell carbon-doped pervious concrete under different addition amounts of the saturated coconut shell carbon. From the table 4 and the table 5, it can be known that the compressive strength of the concrete can be obviously increased by doping the saturated coconut shell carbon in the same curing age, and the permeability coefficient of the concrete cannot be obviously changed by adding the saturated coconut shell carbon, so that the potential of the saturated coconut shell carbon in reducing runoff rainwater is proved. This demonstrates that the designed coconut shell doped concrete with different water-cement ratios has good compression resistance and water permeability.|[0077] TABLE 4 compressive Strength of saturated Cocos Nucifera carbon-doped pervious concrete|[0078] |[0079] TABLE 5 Permeability coefficient of saturated coconut shell carbon-doped pervious concrete|[0080] |[0081] |[0082] Specific example 4|[0083] Preferably selecting saturated water coconut shell carbon with the addition of 0-50 parts of the coconut shell carbon, preparing the saturated water coconut shell carbon doped pervious concrete, and applying the saturated water coconut shell carbon doped pervious concrete to a pervious paving system. As shown in fig. 5, five water permeable paving devices are designed. Adopt PVC material experimental box (the size is 300mm x 1000 mm), every box sets up the delivery port in the bottom to be provided with the sample connection, like sample connection 1, sample connection 2, sample connection 3 and sample connection 4 in figure 5. The filling materials are a pervious concrete layer 10, a base layer 20, an underlayer 30 and a soil matrix 40 from top to bottom in sequence. The material of the base layer 20 may be gravel and the material of the sub-base layer 30 may be crushed stone. In order to use the water-cement ratio of 1:3 as five kinds of concrete layer 10 that permeates water, use the rainfall simulation device to carry out artifical rainwater simulation the concrete layer 10 that permeates water purifies to the runoff rainwater in practical application. The flow is adjusted by the peristaltic pump, simulated runoff with proper concentration is prepared by tap water and medicines (shown in table 6), then the electric mixer works for 30min to ensure complete mixing, the peristaltic pump is started to adjust to proper flow rate, the time is recorded to control the water inflow, and manual water distribution is uniformly distributed on a pavement surface layer through the spray head with set strength. Referring to the rainfall in Beijing, 560L (liter) of total inflow of each paving system is designed, and the inflow of the system in two years (280 multiplied by 2= 560L) is simulated.|[0084] TABLE 6 Water concentration of contaminants|[0085] |[0086] FIG. 6 is a coconut shell carbon doped pervious concrete facing pair with different saturated coconut shell carbon additions according to the present invention(Ammonia nitrogen) removal effect. FIG. 7 shows the effect of coconut shell carbon doped pervious concrete facing on COD (chemical oxygen demand) removal at different saturated water coconut shell carbon addition levels according to the present invention. FIG. 8 shows the TN (total nitrogen) removal effect of the coconut shell carbon-doped pervious concrete surface layer under different saturated water coconut shell carbon addition amounts. FIG. 9 shows the TP (total phosphorus) removal effect of the coconut shell carbon-doped pervious concrete surface layer under different saturated water coconut shell carbon addition amounts. FIG. 10 shows the NO ratio of coconut shell charcoal-doped pervious concrete facing layer pair at different saturated coconut shell charcoal addition levels according to the present invention 3 The effect of removing N (nitrate nitrogen). The results in FIGS. 6 to 10 show that after adding saturated coconut shell charcoal, the pervious concrete surface layer material is paired with/or matched with a->COD、TN、TP、NO 3 The removal rate of-N is increased, wherein the coconut shell carbon is doped to 25 parts by weight of the pervious concrete of saturated coconut shell carbon>COD、TN、TP、NO 3 The best N removal effect is achieved, 50%, 42.33%, 54.78%, 24.8% and 50% removal rate are respectively achieved, and the removal rate is increased by 27.5%, 9.88%, 20.87%, 9.6% and 16.67% compared with that of the permeable concrete without the saturated coconut shell carbon, which shows that the permeable concrete doped with the saturated coconut shell carbon improves the purification effect of the permeable pavement surface layer on conventional pollutants in radial flow pollution.|[0087] FIG. 11 shows the effect of removing heavy Cu (copper) from the coconut shell carbon-doped pervious concrete surface layer at different amounts of saturated coconut shell carbon according to the present invention. FIG. 12 shows the effect of removing heavy Pb (lead) from the coconut shell charcoal-doped pervious concrete surface layer at different amounts of saturated coconut shell charcoal according to the present invention. FIG. 13 shows the effect of removing heavy Zn (Zn) from the coconut shell carbon-doped pervious concrete surface layer at different amounts of saturated coconut shell carbon. As can be seen from fig. 11 to 13, the saturated water coconut shell carbon doped permeable concrete applied to the permeable pavement surface material has good effect on removing heavy metal pollution, another main pollutant in simulated runoff. After the saturated coconut shell carbon is added, the removal rate of the permeable concrete surface layer material on Cu, pb and Zn is increased, wherein the removal rate of the saturated coconut shell carbon-doped permeable concrete with the coconut shell carbon in 25 parts by weight on Cu, pb and Zn is optimal and reaches 51.25%, 48.21% and 49.13% respectively, and the removal rate of the saturated coconut shell carbon-doped permeable concrete is increased by 14.17%, 14.28% and 20% compared with the removal rate of the saturated coconut shell carbon-not-added permeable concrete on Cu, pb and Zn, which shows that the saturated coconut shell carbon-doped permeable concrete also improves the purification effect of the permeable pavement surface layer on heavy metal pollutants in radial flow pollution.|[0088] The invention further provides a method for treating runoff pollutants by using the pervious concrete with the functions of reducing pollution and carbon (namely the coconut shell carbon doped pervious concrete), which comprises the following steps:|[0089] s1', providing the pervious concrete with the functions of reducing pollution and carbon;|[0090] and S2', applying the pervious concrete with the functions of reducing pollution and carbon in sponge city construction to purify rainwater pollution.|[0091] The method for treating runoff pollutants by using the pervious concrete with the functions of reducing pollution and carbon has the advantages of good adsorption performance, high pollutant treatment efficiency and the like, and is a widely adopted method for treating runoff pollution of rainwater.|[0092] The foregoing descriptions of specific exemplary embodiments of the present invention have been presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain certain principles of the invention and its practical application to enable one skilled in the art to make and use various exemplary embodiments of the invention and various alternatives and modifications as are suited to the particular use contemplated. It is intended that the scope of the invention be defined by the claims and their equivalents. (CN115838267)|TECHNICAL FIELD|[0001] The invention belongs to the field of environmental ecological engineering, and particularly relates to a preparation method and application of novel pervious concrete with functions of reducing pollution and carbon.|BACKGROUND ART|[0002] As a new generation of urban rainfall flood management concept, the sponge city is newly built with various rainwater and accumulated water absorption, purification and dredging facilities, so that the city has toughness and elasticity like sponge, and has positive effects on repairing city water ecology, conserving water resources, enhancing city waterlogging prevention capacity and reducing runoff pollution. The ecological civilization construction of China enters the key period of taking carbon reduction as a key strategic direction, promoting pollution and carbon reduction synergistic interaction, promoting the development of economic society and comprehensive green transformation and realizing the quality improvement of ecological environment from quantitative change to qualitative change. Therefore, how to construct sponge cities on the basis of low carbon is the key point of low carbon ecological construction.|[0003] With the rapid development of urbanization, rainwater runoff has developed into a main factor of urban non-point source pollution. The pervious concrete is one of main technical measures of 'seepage' in sponge city construction, can effectively reduce runoff pollution load, and achieves the effects of purifying water quality and improving urban water environment. However, the carbon emission of the pervious concrete in the production and transportation process is not negligible. Therefore, the construction method is a feasible road for constructing the sponge city with low carbon, reducing the whole carbon footprint of the pervious concrete, and improving the carbon fixing capacity and decontamination effect of the pervious concrete.|DISCLOSURE|Disclosure of Invention|[0004] In view of the above, the invention provides a preparation method and application of a novel pervious concrete with pollution-reducing and carbon-reducing functions for reducing the overall carbon footprint of the pervious concrete, improving the carbon fixing capacity and the decontamination and purification effects of the pervious concrete. In the preparation method and application of the novel pervious concrete with pollution-reducing and carbon-reducing functions, the coconut shell carbon is sealed in the pervious concrete, so that carbon sealing is realized, and the effect of reducing carbon is achieved; meanwhile, the prepared coconut shell carbon-doped pervious concrete has a porous structure, is beneficial to adsorbing and removing pollutants, and can realize a purification function on rainwater runoff pollution by applying the coconut shell carbon-doped pervious concrete to sponge city construction, so that pollution reduction and carbon reduction synergistic effect is realized.|[0005] A preparation method of pervious concrete with pollution-reducing and carbon-reducing functions comprises the following steps: pyrolyzing and carbonizing coconut shells in an anoxic environment to obtain coconut shell carbon; enabling the coconut shell carbon to absorb water and saturate to obtain saturated water coconut shell carbon; and stirring the saturated water coconut shell carbon, cement, gravel, water and a high-efficiency water reducing agent according to a certain mass ratio, wherein the mass ratio of the coconut shell carbon, the cement, the gravel, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 5 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent.|[0006] Further, before pyrolyzing and carbonizing the coconut shells in an anoxic environment, the coconut shells are placed in a cool and ventilated environment for air drying treatment, so that the moisture of the coconut shells is reduced to be below 20%, and then the air-dried coconut shells are crushed to obtain crushed materials with the length of 2 cm-3 cm.|[0007] Further, the oxygen-deficient environment is formed by introducing inert gas or vacuumizing; and/or, the temperature for pyrolyzing and carbonizing the coconut shell is 500-750 ℃; and/or increasing the temperature to 500-750 ℃ at a rate of 10 ℃/min and staying at 500-750 ℃ for 0.5-8 h.|[0008] Further, before the coconut shell charcoal is saturated by absorbing water, the coconut shell charcoal is put into a ball mill to be crushed for 30min and then passes through a 200-mesh screen to obtain coconut shell charcoal powder.|[0009] Further, the preparation method of the saturated coconut shell carbon comprises the following steps: adding 1 part of coconut shell carbon into 2 parts of water, and stirring for 60-90 s; and adding 1 part of water, and stirring for 15-30 s until the mixture is pasty to obtain the saturated coconut shell carbon.|[0010] Further, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 25 parts of coconut shell carbon, 1000 parts of cement, 3500 parts of broken stone, 300 parts of water and 7.5 parts of a high-efficiency water reducing agent in the saturated water coconut shell carbon; or 25 parts of coconut shell carbon, 1000 parts of cement, 3500 parts of broken stone, 280 parts of water and 7.5 parts of a high-efficiency water reducing agent in the saturated water coconut shell carbon.|[0011] Further, the mass ratio of the water to the cement is 1:2 to 1:5.|[0012] further, the process of stirring the saturated coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent according to a certain mass ratio comprises the following steps: firstly, adding all the broken stones into a concrete stirring device, stirring for 15s to 30s, then adding 1/2 of water, and stirring for 30s to 60s; adding all cement and the rest 1/2 of water, and continuously stirring for 30-60 s; and finally, adding the saturated coconut shell carbon, and stirring for 60 to 90 seconds until the mixture reaches a flowing state to obtain the pervious concrete with the functions of reducing pollution and carbon.|[0013] Further, after the saturated coconut shell carbon, cement, broken stone, water and the high-efficiency water reducing agent are stirred according to a certain mass ratio, the method comprises the following steps: die filling and forming; and demolding, and carrying out standard curing in a standard curing room for a period of time.|[0014] A method of treating runoff contaminants comprising the steps of: providing the pervious concrete with the functions of reducing pollution and carbon; and applying the pervious concrete with the functions of reducing pollution and carbon in sponge city construction to purify rainwater pollution.|[0015] Compared with the prior art, the preparation method and the application of the pervious concrete with the functions of reducing pollution and carbon have the following advantages:|[0016] firstly, the coconut shell carbon is doped or sealed in the pervious concrete, so that the agricultural solid waste recovery can be effectively promoted, the utilization rate of agricultural wastes can be effectively improved, andthe carbon fixation capacity and the possibility of greatly reducing the land area required by waste disposal are achieved, and the ecological benefit is very obvious. Meanwhile, the coconut shell charcoal can reduce about 870 kilograms of CO per ton of dry raw material according to the type of the raw material and the preparation conditions 2 Equivalent net greenhouse gas emissions, with 62% to 66% being achieved by carbon capture and storage of biomass feedstock of coconut shell char. Compared with the prior sealing and storing technology, the method has the advantages that the coconut shell carbon is sealed and stored in the pervious concrete, the operation is simple, and the carbon sealing and storing can be effectively realized. Coconut charcoal is a very good CO due to its affinity for non-polar compounds and high proportion of surface pores 2 The adsorbent has good advantages for isolating carbon in pervious concrete;|[0017] secondly, the coconut shell carbon has the characteristic of surface roughness, can promote the adhesion of the coconut shell carbon and pervious concrete slurry, has the capacity of building a bridge between micropores on an interface transition area and hydration products, and is beneficial to redistribution of stress. Therefore, the coconut shell charcoal can avoid the brittle failure of pervious concrete. In addition, the water absorption and retention performance of the coconut shell carbon can improve the water evaporation and shrinkage resistance of the pervious concrete slurry, and meanwhile, the moisture contained in the coconut shell carbon can promote the hydration process of the pervious concrete, so that the compressive strength of the pervious concrete is improved. The coconut shell carbon is doped into the pervious concrete, so that the basic performance of the pervious concrete can be effectively enhanced. In addition, pervious concrete is used as a common material in sponge city construction, and is mostly used for absorbing rainwater runoff and reducing runoff pollution. The permeable concrete doped with coconut shell carbon can further improve the dirt cleaning capability of the permeable concrete, thereby realizing the dual functions of carbon fixation and pollution reduction. Therefore, the coconut shell carbon doped pervious concrete has the functions of reducing pollution and carbon;|[0018] thirdly, coconut shell charcoal is a carbonaceous material which takes agricultural wastes as raw materials and can be produced by various processes. The coconut shell carbon is partially doped into the concrete, so that the micro-filler and the internal curing effect can be exerted, the mechanical property and the durability of the concrete are improved, the stable carbon element is stored in the concrete, and the permanent sealing can be realized, so that the aim of reducing carbon is fulfilled;|[0019] and fourthly, the coconut shell carbon is used as an efficient environment adsorption material, multiple adsorption and purification mechanisms are provided for target pollutants, the rainwater runoff pollution purification capacity of the coconut shell carbon can be further enhanced, and important help is provided for coordinating rainwater flood management, reducing runoff pollution and constructing a low-carbon sponge city. Therefore, the coconut shell carbon is added into the pervious concrete, so that the system effect can be exerted to the maximum extent, the resource utilization and carbon source recycling of agricultural wastes are realized, the requirements of pollution reduction and carbon reduction are met, and the coconut shell carbon permeable concrete has extremely high application value and practical significance;|[0020] fifthly, the coconut shell carbon doped pervious concrete has low preparation cost and high performance;|[0021] and sixthly, the method for treating runoff pollutants by using the pervious concrete with the functions of reducing pollution and carbon has the advantages of good adsorption performance, high pollutant treatment efficiency and the like, and is a widely adopted method for treating runoff pollution of rainwater.|DRAWINGS DESCRIPTION|[0022] FIG. 1 is a flow chart of a preparation method of pervious concrete with pollution-reducing and carbon-reducing functions provided by the invention.|[0023] FIG. 2 is a flow chart of the method for preparing coconut shell charcoal from agricultural wastes provided by the invention.|[0024] FIG. 3 is a Scanning Electron Microscope (SEM) photograph of coconut shell carbon provided by the present invention.|[0025] FIG. 4 is an SEM photograph of a pervious concrete slurry provided by the present invention after doping with coconut shell carbon.|[0026] Fig. 5 is a schematic structural diagram of the water permeable paving device for simulating the effect of removing pollutants according to the present invention.|[0027] FIG. 6 is a coconut shell carbon-doped pervious concrete facing pair with different coconut shell carbon addition amounts according to the present invention(Ammonia nitrogen) removal effect.|[0028] FIG. 7 shows the effect of coconut shell carbon doped pervious concrete surface layer on COD (chemical oxygen demand) removal at different coconut shell carbon addition levels.|[0029] FIG. 8 shows the TN (total nitrogen) removal effect of the coconut shell carbon-doped pervious concrete surface layer provided by the present invention at different coconut shell carbon addition levels.|[0030] FIG. 9 shows the TP (total phosphorus) removal effect of the coconut shell carbon-doped pervious concrete surface layer under different coconut shell carbon addition amounts.|[0031] FIG. 10 shows the NO ratio of the coconut shell carbon-doped pervious concrete surface course under different coconut shell carbon addition amounts 3 The effect of removing N (nitrate nitrogen).|[0032] FIG. 11 shows the effect of removing Cu (copper) from the coconut shell carbon doped pervious concrete surface layer at different addition levels of coconut shell carbon.|[0033] FIG. 12 shows the effect of removing heavy Pb (lead) from the coconut shell carbon-doped pervious concrete surface layer at different amounts of coconut shell carbon.|[0034] FIG. 13 shows the effect of removing heavy Zn (Zn) from the coconut shell carbon doped pervious concrete surface layer at different addition amounts of coconut shell carbon.|[0035] Description of the main reference numerals:|[0036] 10-a pervious concrete layer; 20-a base layer; 30-an underlayer; 40-soil base; 1-a sampling port; 2-a sampling port; 3-a sampling port; 4-sampling port.|INVENTION MODE|Detailed Description|[0037] The technical solution of the present invention will be described below by way of specific examples. It is to be understood that one or more of the steps referred to in the present application do not exclude the presence of other methods or steps before or after the combination of steps, or that other methods or steps may be intervening between those steps specifically referred to. It should also be understood that these examples are intended only to illustrate the invention and are not intended to limit the scope of the invention. Unless otherwise indicated, the numbering of the method steps is only for the purpose of identifying the method steps, and is not intended to limit the arrangement order of each method or the scope of the implementation of the present invention, and changes or modifications of the relative relationship thereof may be regarded as the scope of the implementation of the present invention without substantial technical change.|[0038] The preparation method and application of the pervious concrete with pollution-reducing and carbon-reducing functions provided by the invention are further explained in the following by combining the attached drawings.|[0039] Referring to fig. 1, the present invention provides a method for preparing a pervious concrete with pollution-reducing and carbon-reducing functions, that is, a method for preparing a coconut shell carbon-doped pervious concrete, comprising the following steps:|[0040] s1, pyrolyzing and carbonizing coconut shells in an anoxic environment to obtain coconut shell carbon; and|[0041] and S2, stirring the coconut shell carbon, cement, broken stone, water and a high-efficiency water reducing agent according to a certain mass ratio to obtain the coconut shell carbon-doped pervious concrete, wherein the coconut shell carbon-doped pervious concrete is the pervious concrete with the functions of reducing pollution and carbon.|[0042] In step S1, preferably, the coconut shell is air-dried before the pyrolysis carbonization, so that the moisture of the coconut shell is reduced to less than 20%. Preferably, the air-dried coconut shell is subjected to mixing and crushing treatment by using a method such as manual crushing, mechanical crushing and the like to obtain crushed material with the length of 2cm (centimeter) to 3 cm.|[0043] In the step S2, the coconut shell is pyrolyzed and carbonized at high temperature in an anoxic environment or an anoxic environment to prepare the coconut shell carbon. Since the coconut shell charcoal is prepared from agricultural waste, the coconut shell charcoal is also referred to as agricultural waste-based coconut shell charcoal. Due to anoxic environment, the agricultural waste is blocked from being converted into carbon dioxide (CO) 2 )。|[0044] In one embodiment, the air-dried and pulverized coconut shells are placed in a quartz boat and placed in a tube furnace for pyrolytic carbonization.|[0045] The oxygen-deficient environment can be formed by introducing inert gas or vacuumizing, and the inert gas comprises argon and the like. In one embodiment, the oxygen deficient environment is formed using an argon purge.|[0046] The temperature for pyrolyzing and carbonizing the coconut shells is 500 ℃ to 750 ℃. In one embodiment, the temperature in the tube furnace is increased to 500 ℃ to 750 ℃ at a rate of 10 ℃/min (degrees/min) and is maintained at 500 ℃ to 750 ℃ for a period of time, i.e., a carbonization time for pyrolytically carbonizing the coconut shell, which is 0.5h (hours) to 8h.|[0047] And the step S2 further comprises the step of crushing and sieving the coconut shell charcoal to obtain coconut shell charcoal powder. Specifically, after the coconut shell charcoal is cooled, the coconut shell charcoal is crushed and sieved to obtain coconut shell charcoal powder, namely agricultural waste-based coconut shell charcoal powder. In one embodiment, the coconut shell charcoal is pulverized by a ball mill, and is sieved by a 40-200 mesh sieve, and after shaking by a shaking machine, a carbon-rich sieved substance is collected, and the sieved substance is the coconut shell charcoal powder.|[0048] And the step S2 further comprises the step of enabling the coconut shell carbon to absorb water and saturate to obtain saturated water coconut shell carbon. That is, it is preferable that before the step S3 "mixing the coconut shell charcoal, the cement, the crushed stone, the water and the high efficiency water reducing agent according to a certain mass ratio" is performed, the coconut shell charcoal is saturated by absorbing water in advance, so as to avoid the coconut shell charcoal from robbing moisture necessary for the hydration of the concrete, and the moisture stored in the saturated coconut shell charcoal can further promote the hydration reaction of the concrete.|[0049] In a specific embodiment, the preparation method of the saturated coconut shell carbon comprises the following steps: adding 1 part of coconut shell carbon into 2 parts of water, and stirring for 60s (seconds) to 90s; and adding 1 part of water, and stirring for 15-30 s until the mixture is pasty, wherein the obtained product is the saturated coconut shell carbon.|[0050] In the step S2, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent is as follows: 0 to 50 parts of coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent. In a specific embodiment, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent is as follows: 0 to 50 parts of coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 5 to 10 parts of high-efficiency water reducing agent. In a specific embodiment, the coconut shell carbon absorbs water to be saturated to become saturated water coconut shell carbon, and the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 0 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent. In a specific embodiment, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 0 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 5 to 10 parts of high-efficiency water reducing agent. Preferably, the coconut shell carbon in the saturated coconut shell carbon can be 5 parts, 6.25 parts, 10 parts, 12.5 parts, 15 parts, 20 parts, 30 parts, 40 parts or 50 parts. In a specific embodiment, the mass ratio of the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent in the saturated water coconut shell carbon is as follows: 5 to 50 parts of coconut shell carbon in the saturated water coconut shell carbon, 1000 parts of cement, 3000 to 5000 parts of broken stone, 200 to 500 parts of water and 0 to 10 parts of high-efficiency water reducing agent.|[0051] The mass ratio of the water to the cement (namely the water cement ratio) is 1:2 to 1:5. the types of the cement, the broken stone and the high-efficiency water reducing agent are not limited. In a specific embodiment, the cement is P.O42.5 type portland cement, the crushed stone is made of basalt, the particle size of the crushed stone is 4.75mm (millimeters) to 9.5mm, the high-efficiency water reducing agent is a polycarboxylic acid water reducing agent, and the water reducing rate of the polycarboxylic acid water reducing agent is not less than 20%.|[0052] In a specific embodiment, the saturated water coconut shell carbon, the cement, the broken stone, the water and the high efficiency water reducing agent are weighed according to a certain mass ratio and placed into a concrete stirring device until the materials are uniformly stirred, so that the novel permeable concrete with the functions of reducing pollution and carbon and having low cost and high performance is prepared.|[0053] In a specific embodiment, the process of stirring the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent according to a certain mass ratio is as follows: firstly, adding all the broken stones into the concrete stirring equipment, stirring for 15s to 30s, then adding 1/2 of water, and stirring for 30s to 60s; adding all the cement and the rest 1/2 of the water, and continuously stirring for 30-60 s; and finally, adding saturated coconut shell carbon, and stirring for 60 to 90 seconds until the mixture reaches a flowing state, thereby obtaining the pervious concrete with the functions of reducing pollution and carbon.|[0054] Further, as shown in fig. 1, after the step S2 "mixing the coconut shell charcoal, the cement, the crushed stone, the water and the high efficiency water reducing agent according to a certain mass ratio", the method for preparing the pervious concrete with the functions of reducing pollution and carbon may further include the following steps:|[0055] s3, stirring the coconut shell carbon, the cement, the broken stone, the water and the high-efficiency water reducing agent according to a certain mass ratio to obtain a mixture, continuously stirring the mixture, and filling and molding the mixture; and|[0056] and S4, demolding, and carrying out standard curing in a standard curing room for a period of time.|[0057] In step S3, in one embodiment, the mixer continuously mixes the mix for 2 minutes and 30 seconds.|[0058] In step S4, in a specific embodiment, standard curing is performed for 28 days to obtain the novel coconut shell carbon-doped permeable concrete with the functions of reducing pollution and carbon.|[0059] The concrete examples of the preparation method of the pervious concrete with the functions of reducing pollution and carbon are as follows.|[0060] Detailed description of the preferred embodiment 1|[0061] FIG. 2 is a flow chart of the process of preparing coconut shell charcoal from the agricultural wastes. In this embodiment, the agricultural waste is coconut shells, and the coconut shells are placed in a cool and ventilated environment for air-drying treatment, so that the moisture content of the coconut shells is reduced to below 20%. And then mechanically crushing the air-dried coconut shells by a crusher to obtain crushed materials with the length of 2cm to 3 cm. Then, the crushed material is placed in a tube furnace, argon is introduced to produce an anaerobic condition, the temperature is raised to 500 ℃ at the speed of 10 ℃/min, and the black carbon-shaped object, namely the coconut shell biochar, is obtained after pyrolysis and carbonization for 30 min. And after cooling, putting the coconut shell biochar into a ball mill for crushing for 30min, then sieving the coconut shell biochar through a 200-mesh sieve, and collecting sieved substances after shaking by a shaking machine to obtain coconut shell carbon powder. Table 1 lists the basic chemical compositions of coconut shell carbon. From table 1, the percentage contents of five elements, phosphorus (P), oxygen (O), silicon (Si), carbon (C), and chlorine (Cl), were found, wherein carbon (C) was 83.7%. Thus, it can be seen from Table 1 that the coconut shell carbon is rich in carbon, which indicates that the coconut shell carbon is a carbon-rich material and that the coconut shell carbon can be effectively fixed by doping the coconut shell carbon into pervious concrete. FIG. 2 is an SEM photograph of coconut shell biochar, and it can be observed from FIG. 2 that the surface pore structure of the coconut shell carbon is more developed, and the specific surface area of the coconut shell carbon is increased, so that the coconut shell carbon is in wider contact with pollutants on one hand, and is more favorable for adsorbing the pollutants; on the other hand, the coconut shell carbon can store more water, is beneficial to the adhesion of cement particles and the coconut shell carbon, and further promotes the hydration reaction of concrete, thereby increasing the hydration products.|[0062] TABLE 1 basic chemical composition of coconut husk charcoal|[0063] Density (g/cm) 3 )P(%)O(%)Si(%)C(%)Cl(%)pH1.473.411.21.383.70.37.59|[0064] Specific example 2|[0065] In this example, the water-cement ratio was designed to be 1: and 3, weighing 1000 parts of cement, 300 parts of water, 3500 parts of broken stone, 0 to 50 parts of coconut shell carbon in the saturated coconut shell carbon and 7.5 parts of high-efficiency water reducing agent according to the mass mixing ratio.|[0066] In the embodiment, the water meets the three types of water quality standards of the surface or better than the three types of water quality standards specified by the national standard GB3838-2002, the cement adopts the golden corner brand P.O42.5 grade ordinary portland cement, and the polycarboxylate water reducer is purchased from the Fine chemical industry Co., ltd.|[0067] In the embodiment, all the crushed stones are added into concrete stirring equipment to be stirred for 15s to 30s, then 150 parts of water is added, and the mixture is stirred for 30s to 60s; adding all cement and 150 parts of water, and continuously stirring for 30-60 s; and finally, adding saturated water coconut shell carbon, wherein the parts of the coconut shell carbon in the saturated water coconut shell carbon are respectively 0, 6.25, 12.5, 25 and 50, stirring for 60-90 s until the mixture reaches a flowing state, and thus obtaining the novel permeable concrete with pollution-reducing and carbon-reducing functions in different doping proportions of the coconut shell carbon. Fig. 4 is an SEM photograph of the pervious concrete slurry provided by the present invention after doping coconut shell carbon. From the microstructure shown in fig. 4, it can be seen that the coconut shell carbon is embedded in the concrete slurry, indicating that the coconut shell carbon doped pervious concrete is successfully prepared.|[0068] The compressive strength and the water permeability coefficient of the pervious concrete are the most basic and important test items in a plurality of performance indexes of the pervious concrete, and the compressive strength and the water permeability coefficient of the prepared test block (namely the saturated coconut shell carbon-doped pervious concrete) are measured according to a test method specified by JC/T2558-2020 permeable concrete. The compressive strength and the water permeability coefficient of the pervious concrete under different addition amounts of the coconut shell carbon and the saturated water coconut shell carbon are respectively shown in the table 2 and the table 3, wherein the reference sample coconut shell carbon is not treated by supersaturated water. It can be seen from table 2 that, as the curing period increases, the compressive strength of the concrete continuously increases with the increase of the content of the saturated water coconut shell carbon in the concrete doped with five different proportions of the saturated water coconut shell carbon, that is, in the same curing period, the compressive strength of the concrete can be obviously increased by doping the saturated water coconut shell carbon, and when the doping amount of the saturated water coconut shell carbon is 25 parts, the compressive strength of the concrete reaches the strongest level. The coconut shell carbon doped with unsaturated water can enhance the compressive strength of concrete in a short term, but reduces the compressive strength of concrete in a long term. Therefore, the saturated coconut shell carbon is more feasible to select. Table 3 shows that the addition of saturated coconut shell carbon does not significantly change the permeability coefficient of concrete, demonstrating its potential in reducing runoff rain.|[0069] TABLE 2 compressive Strength of coconut carbon-doped pervious concrete and saturated coconut carbon-doped pervious concrete|[0070] |[0071] TABLE 3 Permeability coefficient of saturated coconut shell carbon-doped pervious concrete|[0072] |[0073] |[0074] Specific example 3|[0075] In this example, the water-cement ratio is designed to be 1:2.8, weighing 1000 parts of cement, 280 parts of water, 3500 parts of broken stone, 0 to 50 parts of coconut shell carbon in the saturated coconut shell carbon and 7.5 parts of high-efficiency water reducing agent according to the mass mixing ratio. The specific materials and methods were the same as in example 2.|[0076] And (3) according to a test method specified by JC/T2558-2020 pervious concrete, measuring the compressive strength and the water permeability coefficient of the prepared test block (namely the saturated coconut shell carbon doped pervious concrete). Tables 4 and 5 show the compressive strength and water permeability coefficient of the saturated coconut shell carbon-doped pervious concrete under different addition amounts of the saturated coconut shell carbon. From the table 4 and the table 5, it can be known that the compressive strength of the concrete can be obviously increased by doping the saturated coconut shell carbon in the same curing age, and the permeability coefficient of the concrete cannot be obviously changed by adding the saturated coconut shell carbon, so that the potential of the saturated coconut shell carbon in reducing runoff rainwater is proved. This demonstrates that the designed coconut shell doped concrete with different water-cement ratios has good compression resistance and water permeability.|[0077] TABLE 4 compressive Strength of saturated Cocos Nucifera carbon-doped pervious concrete|[0078] |[0079] TABLE 5 Permeability coefficient of saturated coconut shell carbon-doped pervious concrete|[0080] |[0081] |[0082] Specific example 4|[0083] Preferably selecting saturated water coconut shell carbon with the addition of 0-50 parts of the coconut shell carbon, preparing the saturated water coconut shell carbon doped pervious concrete, and applying the saturated water coconut shell carbon doped pervious concrete to a pervious paving system. As shown in fig. 5, five water permeable paving devices are designed. Adopt PVC material experimental box (the size is 300mm x 1000 mm), every box sets up the delivery port in the bottom to be provided with the sample connection, like sample connection 1, sample connection 2, sample connection 3 and sample connection 4 in figure 5. The filling materials are a pervious concrete layer 10, a base layer 20, an underlayer 30 and a soil matrix 40 from top to bottom in sequence. The material of the base layer 20 may be gravel and the material of the sub-base layer 30 may be crushed stone. In order to use the water-cement ratio of 1:3 as five kinds of concrete layer 10 that permeates water, use the rainfall simulation device to carry out artifical rainwater simulation the concrete layer 10 that permeates water purifies to the runoff rainwater in practical application. The flow is adjusted by the peristaltic pump, simulated runoff with proper concentration is prepared by tap water and medicines (shown in table 6), then the electric mixer works for 30min to ensure complete mixing, the peristaltic pump is started to adjust to proper flow rate, the time is recorded to control the water inflow, and manual water distribution is uniformly distributed on a pavement surface layer through the spray head with set strength. Referring to the rainfall in Beijing, 560L (liter) of total inflow of each paving system is designed, and the inflow of the system in two years (280 multiplied by 2= 560L) is simulated.|[0084] TABLE 6 Water concentration of contaminants|[0085] |[0086] FIG. 6 is a coconut shell carbon doped pervious concrete facing pair with different saturated coconut shell carbon additions according to the present invention(Ammonia nitrogen) removal effect. FIG. 7 shows the effect of coconut shell carbon doped pervious concrete facing on COD (chemical oxygen demand) removal at different saturated water coconut shell carbon addition levels according to the present invention. FIG. 8 shows the TN (total nitrogen) removal effect of the coconut shell carbon-doped pervious concrete surface layer under different saturated water coconut shell carbon addition amounts. FIG. 9 shows the TP (total phosphorus) removal effect of the coconut shell carbon-doped pervious concrete surface layer under different saturated water coconut shell carbon addition amounts. FIG. 10 shows the NO ratio of coconut shell charcoal-doped pervious concrete facing layer pair at different saturated coconut shell charcoal addition levels according to the present invention 3 The effect of removing N (nitrate nitrogen). The results in FIGS. 6 to 10 show that after adding saturated coconut shell charcoal, the pervious concrete surface layer material is paired with/or matched with a->COD、TN、TP、NO 3 The removal rate of-N is increased, wherein the coconut shell carbon is doped to 25 parts by weight of the pervious concrete of saturated coconut shell carbon>COD、TN、TP、NO 3 The best N removal effect is achieved, 50%, 42.33%, 54.78%, 24.8% and 50% removal rate are respectively achieved, and the removal rate is increased by 27.5%, 9.88%, 20.87%, 9.6% and 16.67% compared with that of the permeable concrete without the saturated coconut shell carbon, which shows that the permeable concrete doped with the saturated coconut shell carbon improves the purification effect of the permeable pavement surface layer on conventional pollutants in radial flow pollution.|[0087] FIG. 11 shows the effect of removing heavy Cu (copper) from the coconut shell carbon-doped pervious concrete surface layer at different amounts of saturated coconut shell carbon according to the present invention. FIG. 12 shows the effect of removing heavy Pb (lead) from the coconut shell charcoal-doped pervious concrete surface layer at different amounts of saturated coconut shell charcoal according to the present invention. FIG. 13 shows the effect of removing heavy Zn (Zn) from the coconut shell carbon-doped pervious concrete surface layer at different amounts of saturated coconut shell carbon. As can be seen from fig. 11 to 13, the saturated water coconut shell carbon doped permeable concrete applied to the permeable pavement surface material has good effect on removing heavy metal pollution, another main pollutant in simulated runoff. After the saturated coconut shell carbon is added, the removal rate of the permeable concrete surface layer material on Cu, pb and Zn is increased, wherein the removal rate of the saturated coconut shell carbon-doped permeable concrete with the coconut shell carbon in 25 parts by weight on Cu, pb and Zn is optimal and reaches 51.25%, 48.21% and 49.13% respectively, and the removal rate of the saturated coconut shell carbon-doped permeable concrete is increased by 14.17%, 14.28% and 20% compared with the removal rate of the saturated coconut shell carbon-not-added permeable concrete on Cu, pb and Zn, which shows that the saturated coconut shell carbon-doped permeable concrete also improves the purification effect of the permeable pavement surface layer on heavy metal pollutants in radial flow pollution.|[0088] The invention further provides a method for treating runoff pollutants by using the pervious concrete with the functions of reducing pollution and carbon (namely the coconut shell carbon doped pervious concrete), which comprises the following steps:|[0089] s1', providing the pervious concrete with the functions of reducing pollution and carbon;|[0090] and S2', applying the pervious concrete with the functions of reducing pollution and carbon in sponge city construction to purify rainwater pollution.|[0091] The method for treating runoff pollutants by using the pervious concrete with the functions of reducing pollution and carbon has the advantages of good adsorption performance, high pollutant treatment efficiency and the like, and is a widely adopted method for treating runoff pollution of rainwater.|[0092] The foregoing descriptions of specific exemplary embodiments of the present invention have been presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain certain principles of the invention and its practical application to enable one skilled in the art to make and use various exemplary embodiments of the invention and various alternatives and modifications as are suited to the particular use contemplated. It is intended that the scope of the invention be defined by the claims and their equivalents. Family Number|(104252674)|104252674|Abstract|(CN115838267 A)|The invention discloses a preparation method and application of novel pervious concrete with pollution reduction and carbon reduction functions , and belongs to the field of environmental ecological engineering . The preparation method comprises the following steps : firstly , pyrolyzing agricultural waste coconut shells in an oxygen - free environment to obtain crushed coconut shell charcoal , and enabling the coconut shell charcoal to absorb water to be saturated to obtain saturated coconut shell charcoal ; the saturated water coconut shell charcoal crushed material is mixed with cement , water and gravel in a certain proportion , then the mixture is put into a mold for standard curing , and the biochar - doped pervious concrete is obtained . The biochar - doped pervious concrete can efficiently purify rainwater runoff pollutants and perform carbon sequestration . According to the invention , resource utilization of agricultural wastes is realized ; the biochar - doped pervious concrete which is low in cement consumption , large in specific surface area , rich in porous structure and high in adsorption capacity is prepared ; the high - efficiency purification of rainwater runoff is realized ; and the goal of assisting carbon neutralization by the carbon sequestration technology is achieved . The biochar - doped pervious concrete has the advantages of being simple to manufacture , low in cost , long in service life , good in water quality purification effect and the like . |IPC codes|(CN115838267 A)|C01B - 032/05 | Materials, metallurgy C01B-032/05|C04B-014/02|C04B-028/04|C04B-111/40 C01B-032/05|C04B-014/02|C04B-028/04|C04B-111/40 CN110922114|CN108726955|CN107721287|CN112876119|CN112441797|KR20220046723|JP2018162620|CN106007539|JP2006043692|KR20050079277 CN110922114 88019151 WHO=Examiner SELF=N CAT=Y|CN108726955 81841480 WHO=Examiner SELF=N CAT=Y|CN107721287 78893188 WHO=Examiner SELF=N CAT=Y|CN112876119 94460192 WHO=Examiner SELF=N CAT=A|CN112441797 93017665 WHO=Examiner SELF=N CAT=A|KR20220046723 99613660 WHO=Examiner SELF=N CAT=A|JP2018162620 81682656 WHO=Examiner SELF=N CAT=A|CN106007539 74364077 WHO=Examiner SELF=N CAT=A|JP2006043692 32361901 WHO=Examiner SELF=N CAT=A|KR20050079277 33905192 WHO=Examiner SELF=N CAT=A 李国新等: &quot;《混凝土工艺学》&quot;, 中国建材工业出版社, pages: 179 - 180 (Cat. A) KR20050079277; JP2006043692; CN106007539; CN107721287; JP2018162620; CN108726955; CN110922114; CN112441797; CN112876119; KR20220046723 REVOKED (CN115838267)|REVOKED DEAD (CN115838267)|DEAD (CN115838267)|LEGAL DETAILS FOR CN115838267|Actual or expected expiration date=2024-11-29|Legal state=DEAD|Status=REVOKED|Event publication date=2022-12-05|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211552550|Application date=2022-12-05|Standardized application number=2022CN-1552550|Event publication date=2023-03-24|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115838267|Publication stage code=A|Publication date=2023-03-24|Standardized publication number=CN115838267|Event publication date=2023-03-24|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-04-11|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-11-29|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRlymWyzWemL1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067061974&ekey=2375&xpn=CN115838267&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=K90LLp9qS3XuSgZo0KuWLZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN115838267)|CN (CN115838267)|NAME=Beijing University of Civil Engineering and Architecture , COUNTRY=CN (CN115838267)|NAME=MINGLIANG XIN;BEIJING PROFESSIONAL INTELLECTUAL PROPERTY AGENCY LTD , REG=11944 (CN115838267)|NAME=ZHANG ZIYANG|NAME=PENG XINYU|NAME=ZHANG XIAOXIAN|NAME=LI FEI|NAME=CHEN HONGRUI|NAME=ZHANG XIAORAN|NAME=TAN CHAOHONG|NAME=LI HAIYAN 0 1 Titre: (CN115838267)|Preparation method and application of pervious concrete with pollution reduction and carbon reduction functions Résumé: (CN115838267)|The invention discloses a preparation method and application of novel pervious concrete with pollution reduction and carbon reduction functions, and belongs to the field of environmental ecological engineering. The preparation method comprises the following steps: firstly, pyrolyzing agricultural waste coconut shells in an oxygen-free environment to obtain crushed coconut shell charcoal, and enabling the coconut shell charcoal to absorb water to be saturated to obtain saturated coconut shell charcoal; the saturated water coconut shell charcoal crushed material is mixed with cement, water and gravel in a certain proportion, then the mixture is put into a mold for standard curing, and the biochar-doped pervious concrete is obtained. The biochar-doped pervious concrete can efficiently purify rainwater runoff pollutants and perform carbon sequestration. According to the invention, resource utilization of agricultural wastes is realized; the biochar-doped pervious concrete which is low in cement consumption, large in specific surface area, rich in porous structure and high in adsorption capacity is prepared; the high-efficiency purification of rainwater runoff is realized; and the goal of assisting carbon neutralization by the carbon sequestration technology is achieved. The biochar-doped pervious concrete has the advantages of being simple to manufacture, low in cost, long in service life, good in water quality purification effect and the like. 87 Abstract gpt-4o-mini no The article focuses on pervious concrete with pollution reduction and carbon reduction functions, which does not involve the accelerated weathering of minerals or direct CO₂ capture through mineral carbonation.
96 CN202210073314 CN202211317927|CN202210073314 CN115445393|CN115445393|CN114522512 100174807 CN115445393 B 2024-04-26 [CN115445393B]|CN115445393 A 2022-12-09 [CN115445393]|CN114522512 A 2022-05-24 [CN114522512] 2022-01-21 2022-10-26|2022-01-21 2024-04-26|2022-12-09|2022-05-24 (CN115445393B)|2024-04-26| (CN115445393)|2042-10-26|(CN114522512)|2022-12-06 (CN115445393)|Method for improving carbon sink efficiency of soil and underground water (CN115445393)|The invention discloses a method for improving the carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increase and carbon cycle improvement. The method comprises the following steps: step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three-dimensional model, and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount; step 2, paving peat soil with a high-adsorbability and high-water-content space to the area selected in the step 1, and wetting the dried peat soil with water before paving; thirdly, holes are formed in the laid peat soil, the permeability of a laid area is enhanced, more earth surface rainfall can enter the soil and underground water space through infiltration, and the CO2 amount adsorbed by the peat soil is increased. Through soil adsorption and rainfall infiltration leaching carrying processes, the content of dissolved inorganic carbon entering the soil and underground water is greatly increased, so that atmospheric CO2 is stored in a deep underground space, the carbon sequestration efficiency of the soil and underground water is improved, and important carbon sequestration significance is achieved. GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN (CN115445393)|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN])|(CN115445393)|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN])|(CN114522512)|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN]) YANG MINGXING|ZHANG MIN|YANG WU|XIE FEI|YAO DUNTING|LI WEI (CN115445393)|YANG MINGXING|ZHANG MIN|YANG WU|XIE FEI|YAO DUNTING|LI WEI|(CN115445393)|YANG MINGXING|ZHANG MIN|YANG WU|XIE FEI|YAO DUNTING|LI WEI (CN115445393)|CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP)|Reg. Nb: 11308|(CN114522512)|CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP)|Reg. Nb: 11308 (CN115445393)|Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.|In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples.| (CN115445393)|1. A method for improving the carbon sink efficiency of soil and underground water is characterized by comprising the following steps: the method comprises the following steps: Firstly, judging and extracting a main rainfall infiltration supplementing area through site GIS analysis and a DEM three-dimensional model to serve as an area for increasing rainfall infiltration; secondly, spreading peat soil with high adsorptivity and high water content to the area selected in the first step, and wetting the dried peat soil with water before spreading; thirdly, inserting holes in the peat soil which is well paved, enhancing the permeability of the paved area, and enabling more surface rainfall to enter soil and groundwater space through infiltration so as to increase the CO 2 absorbed by the peat soil; And fourthly, increasing the water infiltration amount by adopting a manual sprinkling or leaching mode in a rainfall-free season, increasing the CO 2 amount adsorbed by peat soil, and absorbing and storing atmospheric CO 2 in soil and underground water to form dissolved inorganic carbon so as to realize the purpose of carbon sink. | (CN115445393)|The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.|The invention discloses a method for improving carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increasing and carbon circulation improving.|The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:| (CN115445393)|GROUND(100,34)|CARBON SINK(100,29)|UNDERGROUND WATER(100,18)|RAINFALL INFILTRATION(100,10)|RAINFALL INFILTRATION REPLENISHMENT ZONE(66,1)|RAINFALL INFILTRATION LEACHING(61,2)|SPREADING PEAT SOIL(55,6)|GROUNDWATER(45,12)|SITE GI ANALYSIS(44,4)|PEAT SOIL DRYING(43,6)|PEAT SOIL(42,22)|ADSORPTIVITY(40,6)|SITE GI(37,4)|INSERTION(36,4)|SPRINKLING(36,1)|SOIL PERFORMANCE(33,1)|INFILTRATION(31,7)|CARBON CIRCULATION(30,2)|PAVED AREA(29,2)|TILED PEAT SOIL(29,2)|PEAT SOIL WETTING(28,2)|SOIL CARBON SEQUESTRATION(25,1)|LEACHING MODE(24,3)|COLLECTION ZONE(22,1)|RAINFALL FREE SEASON(21,3)|SURFACE RAINFALL(19,6)|DEM THREE DIMENSIONAL MODEL(18,4)|HCO3 ION(18,4)|CARBON SINK SIGNIFICANCE(18,2)|PAVING THICKNESS(18,2)|FLOW CIRCULATION MODE(17,1)|GULLY(14,2)|SOIL ADSORPTION(14,2)|DEEP UNDERGROUND SPACE(13,4)|DEPRESSION(12,4)|WATER INFILTRATION(12,3)|3D MODEL(11,4)|DISSOLVED INORGANIC CARBON(10,15)|PAVED REGION PERMEABILITY(10,2)|SOIL RAINFALL INFILTRATION CHANNEL(10,1)|RAINFALL INFILTRATION FLUSHING ACTION(9,1)|RAINFALL SURFACE RUNOFF(8,7)|SOIL PHYSICAL MODIFIER(8,2)|DISSOLVED INORGANIC CARBON CONTENT(7,3)|SOIL ADSORPTION CAPACITY(7,1)|RAINFALL INFILTRATION SUPPLY AREA(6,4)|WELL PAVED PEAT SOIL(6,2)|ADSORPTIVE ABSORPTION(6,1)|ATMOSPHERIC RAINFALL(6,1)|CARBON SINK ECONOMIC PROSPECT(6,1)|RAINFALL INFILTRATION REPLENISHMENT AREA(6,1)|SOIL ADSORPTION PERFORMANCE(6,1)|COLLECTION AREA(5,6)|POROSITY(5,3)|CARBON NEUTRALIZATION(5,2)|FORMED INSERTION HOLE(5,2)|SPRINKLING MODE(5,2)|ECONOMY DEVELOPMENT(5,1)|RAINFALL INFILTRATION CAPACITY(5,1)|DITCH(4,2)|SPREADING THICKNESS(4,2)|STAINLESS STEEL STICK(4,2)||(CN115445393)|GROUND(100,44)|UNDERGROUND WATER(100,26)|CARBON SEQUESTRATION(100,13)|PRECIPITATION INFILTRATION(100,1)|LEAD PRECIPITATION INFILTRATION(89,1)|SPREAD PEAT SOIL(84,4)|RAINFALL INFILTRATION PERFORMANCE(83,1)|SOLUTIONTHE INORGANIC CARBON(83,1)|PERMEABILITY ENHANCEMENT(82,2)|UNDERGROUND WATERTHE CARBON SEQUESTRATION(76,1)|LEAD RAINFALL INFILTRATION(67,1)|PEAT SOIL(63,21)|PEAT SOIL DRYING(63,6)|RECYCLING CARBON(60,1)|RAINFALL(59,12)|ADSORBABILITY(58,6)|INFILTRATION(47,6)|RAINFALL INFILTRATION RECHARGE AREA(47,1)|GROUNDWATER CARBON SEQUESTRATION(46,1)|SITE GI ANALYSIS(46,1)|REPLENISHMENT AREA(44,2)|TILED PEAT SOIL(43,2)|FUNCTION MANUAL SPRINKLING(43,1)|SOIL ADSORPTION(42,2)|PEAT SOIL WETTING(41,2)|ATMOSPHERIC RAINFALL(39,3)|CARBON SEQUESTRATION SIGNIFICANCE(35,2)|ADSORPTION FUNCTION(35,1)|SPREADING PEAT SOIL(34,3)|SPREADING AREA(33,2)|GROUNDWATER(32,3)|MODE FUNCTION MANUAL SPRINKLING(32,1)|DEM THREE DIMENSIONAL MODEL(27,4)|FLOW CIRCULATION MODE(26,1)|GROUND SURFACE(25,6)|CARBON SINK(22,25)|SPREADING THICKNESS(22,3)|EFFICIENCY FUNCTION(22,2)|JIG(21,2)|CARBON SEQUESTRATION EFFICIENCY FUNCTION(21,1)|RAINFALL INFILTRATION ELUVIATION(20,1)|GULLY(19,4)|RAINFALL INFILTRATION REPLENISHMENT REGION(19,2)|DISSOLVED INORGANIC CARBON(17,24)|DEPRESSION(17,4)|3D MODEL(16,4)|WATER INFILTRATION(16,3)|ROTARY TRANSFORMER(16,1)|RAINFALL INFILTRATION REPLENISHMENT AREA(15,3)|STORAGE FUNCTION(15,1)|FIELD GI ANALYSIS(14,3)|COLLECTION AREA(13,4)|HCO(13,4)|RAINFALL SURFACE RUNOFF(12,6)|FIELD GI(12,3)|RAINFALL INFILTRATION CHANNEL(12,1)|RAINFALL INFILTRATION PASSAGE(12,1)|ADSORPTION PERFORMANCE(10,3)|RAINFALL INFILTRATION CAPACITY(10,2)|ECONOMIC PROSPECT(10,1)|ATMOSPHERIC ABATEMENT(9,1)|CREATIVE EFFORT(9,1)|ADSORPTION CAPACITY(8,2)|CARBON NEUTRALIZATION(8,2)|DIAMETER FUNCTION(7,4)|POROSITY(7,3)|COLLECTION REGION(6,2)|PERMEABILITY(6,2)|RETENTION PERFORMANCE(6,2)|SPRAYING MODE(6,2)|STAINLESS STEEL ROD(6,2)||(CN114522512)|CARBON SINK(100,30)|AQUATIC PHOTOSYNTHESIS(100,12)|AQUATIC CARBON SINK(100,5)|AQUATIC ANIMAL(100,2)|CARBON SINK CAPACITY(100,2)|DIC FERTILIZATION(69,1)|AQUATIC CARBON SEQUESTRATION(61,1)|ATMOSPHERIC CO2IN(51,1)|AQUATIC CARBON(50,4)|RAINWATER(49,13)|GASEOUS FORM2IS(44,3)|CARBON CIRCULATION(42,1)|RAIN WATER GUIDE(41,1)|INORGANIC CARBON(40,11)|LAND CARBONATE(40,6)|LAND CARBONATE WEATHERING(38,3)|SOIL2STORAGE CAPACITY(38,3)|POPULARIZATION(37,1)|RAINFALL(35,13)|SOIL2ENRICHING(35,4)|RAINFALL INFILTRATION(33,6)|FIELD2THE PEAT SOIL(32,3)|AQUATIC PLANT(31,11)|AQUATIC(29,3)|ATMOSPHERIC RAINFALL(28,3)|SOIL PORE(27,8)|RAINFALL AREA(27,3)|CARBON SEQUESTRATION(26,5)|DISSOLVED INORGANIC CARBON(25,25)|GROUNDWATER(25,9)|SINK(25,4)|TERM SCHEMATIC REPRESENTATION(25,1)|ATMOSPHERE2WITHOUT(23,2)|NATURAL CONDITION(23,1)|STABLE ORGANIC CARBON SINK(21,1)|GROUND LAYER(20,6)|CARBON SINK SIGNIFICANCE(20,2)|AQUATIC PHOTOSYNTHETIC ORGANISM PRODUCTIVITY(17,1)|ORGANIC CARBON SINK(16,2)|UNDERGROUND WATER(15,4)|WATERTHE BIOMASS DIC(15,1)|DREDGE(14,3)|INORGANIC CARBON VOLUME(14,3)|PASSAGEWAY(14,3)|POROSITY(14,3)|LAYING(14,1)|ORGANIC CARBON(13,11)|CARBON SINK FORMATION(13,2)|WATER BODY(10,20)|HCO(10,5)|ATMOSPHERIC CO2THE PATHWAY(10,1)|UNCHANGING RAINFALL CONDITION PREMISE(10,1)|PHYTOPLANKTON PRODUCTIVITY(9,1)|DISSOLVED INORGANIC CARBON CONTENT(8,2)|DISSOLVED INORGANIC CARBON SOURCE(7,5)|SURFACE RUNOFF(7,4)|ATMOSPHERIC CO2STORED(7,1)|LAND AQUATIC ECOSYSTEM(7,1)|ATMOSPHERIC CO2AND(6,1)|CARBON SINK ECONOMIC PROSPECT(6,1)|CARBONATE WEATHERING CARBON(6,1)|CREATIVE EFFORT(6,1)|NATIONAL CARBURANT(6,1)|RAW MATERIAL(6,1)|CARBONATE ROCK CONTENT(5,1)|CO2THE KEY(5,1)|DIC PROMINENT SOURCE(5,1)|UNDERGROUND ENVIRONMENT(5,1)|SURFACE WATER(4,20)|STEP THREE(4,3)|PEAT SOIL(4,2)|CARBON NEUTRALIZATION(4,1)|CO2THEREFORE(4,1)|FUNDAMENTAL KEY(4,1)|LIGHT PARTICIPATION(4,1)|PHOTOSYNTHESIS2WITH(4,1)|ALKALINITY(3,1)| (CN115445393)|1. A method for improving the carbon sink efficiency of soil and underground water is characterized by comprising the following steps: the method comprises the following steps:| Firstly, judging and extracting a main rainfall infiltration supplementing area through site GIS analysis and a DEM three-dimensional model to serve as an area for increasing rainfall infiltration; | secondly, spreading peat soil with high adsorptivity and high water content to the area selected in the first step, and wetting the dried peat soil with water before spreading; | thirdly, inserting holes in the peat soil which is well paved, enhancing the permeability of the paved area, and enabling more surface rainfall to enter soil and groundwater space through infiltration so as to increase the CO 2 absorbed by the peat soil; | And fourthly, increasing the water infiltration amount by adopting a manual sprinkling or leaching mode in a rainfall-free season, increasing the CO 2 amount adsorbed by peat soil, and absorbing and storing atmospheric CO 2 in soil and underground water to form dissolved inorganic carbon so as to realize the purpose of carbon sink. |2. A method for enhancing the efficiency of carbon sequestration of soil and groundwater according to claim 1, wherein the primary rainfall infiltration replenishment zone in the first step is designated as a rainfall surface runoff collection zone comprising gullies and depressions created by rainfall.|3. The method for improving the carbon sequestration efficiency of soil and groundwater according to claim 1, wherein the step of spreading peat soil in the second step comprises the steps of: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.|4. The method for improving the carbon sequestration efficiency of soil and groundwater according to claim 1, wherein the third step of inserting holes in the tiled peat soil comprises the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.|5. The method of claim 1, wherein the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions. (CN115445393)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of increasing carbon sink and improving carbon circulation, and particularly relates to a method for improving carbon sink efficiency of soil and underground water.|BACKGROUND ART|[0002] The aim of China is to realize the aims of carbon reaching peak and carbon neutralization in 2030 and 2060 respectively, and increasing the carbon yield and reducing the carbon emission are the most urgent means for realizing the two aims. However, under the current international economic pressure, the promotion of emission reduction work has certain difficulty in order to ensure good development of economy. Thus, adding carbon sinks or finding new ways of carbon sinks is an important ring to achieve both goals. Carbon sequestration is a mechanism for removing CO 2 from the atmosphere, i.e., absorbing CO 2 from the atmosphere into ecosystems such as land and sea and storing it. Wherein, the soil and the groundwater can form the atmospheric CO 2 into dissolved inorganic carbon (mainly comprising several forms, namely dissolved CO 2(aq)、HCO3- ions and CO 32- ions) through the karst action of rock and the hydrolytic action of CO 2 and water. The part of the formed dissolved inorganic carbon mainly enters soil and underground space through a rainfall infiltration channel under the action of rainfall infiltration flushing and is stored to form a carbon sink process for reducing atmospheric CO 2. In this process, two steps are particularly important, namely, the absorption of CO 2 by the soil, and the surface soil has larger pores and can absorb and store atmospheric CO 2. But the soil has different properties, and the porosity and the adsorption capacity are different; secondly, if CO 2 adsorbed and stored by soil does not enter the deep underground space or enters the dynamic underground water space in time, the CO 2 returns to the atmosphere again, carbon sinks cannot be formed, and the main driving force of the process is leaching effect of rainfall infiltration, namely the amount of the rainfall infiltration into the underground water needs to be increased, so that the amount of the CO 2 entering the deep underground space can be increased more, and more carbon sinks are formed.|[0003] Therefore, the method for improving the carbon sink efficiency of the soil and the underground water is developed to perfect the engineering technology of carbon sink improvement in China and improve the practical application prospect of the carbon sink.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.|[0005] In order to solve the technical problems, the invention is realized by the following technical scheme:|[0006] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps: |[0007] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; |[0008] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 45% -55%; |[0009] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; |[0010] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. |[0011] Preferably, the main rainfall infiltration replenishment area in the first step is used as a rainfall surface runoff collection area, and the rainfall surface runoff collection area comprises a gully and a depression formed by rainfall.|[0012] Preferably, the step of spreading peat soil in the second step specifically includes the following steps: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.|[0013] Preferably, the inserting holes on the tiled peat soil in the third step specifically include the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.|[0014] Preferably, the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions.|[0015] Preferably, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other of which is atmospheric CO 2 absorbed by the soil.|[0016] The invention has the following beneficial effects:|[0017] According to the invention, the content of dissolved inorganic carbon entering the soil and underground water can be greatly increased through the carrying process of soil adsorption and rainfall infiltration leaching, so that atmospheric CO 2 is stored in a deep underground space, the carbon sink efficiency of the soil and underground water is improved, the method has important carbon sink significance, the efficient removal of CO 2 in the atmosphere can be realized, and the environmental negative effect can not be generated. |[0018] Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.|INVENTION MODE|Detailed Description|[0019] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0020] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:|[0021] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; |[0022] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 50%; |[0023] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; |[0024] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. |[0025] According to statistical analysis, the higher the adsorption performance of the soil is, the stronger the adsorption capacity of the soil to atmospheric CO 2 is; in addition, the more rainfall infiltration channels of the soil are, the stronger the rainfall infiltration capacity is, and the more CO 2 is carried by rainfall infiltration, so that the content of dissolved inorganic carbon entering a water body can be effectively increased by 2-3 times by a method of increasing the adsorption quantity of CO 2 in the soil and the rainfall infiltration quantity, and the formed carbon sink quantity is increased by 2-3 times, thereby having important carbon sink economic prospects.|[0026] In this example, the Dissolved Inorganic Carbon (DIC) includes dissolved CO 2、HCO3- ions and CO 32- ions.|[0027] In this embodiment, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other is atmospheric CO 2 absorbed by the soil.|[0028] Increasing the dissolution into the soil and the groundwater is fundamental key to increasing carbon sequestration. While there are two sources of Dissolved Inorganic Carbon (DIC) in soil and groundwater, the highly adsorptive absorption of atmospheric CO 2 by peat soil and the infiltration leaching of atmospheric rainfall carry the absorbed dissolved inorganic carbon. The two parts realize the purposes of reducing, transferring and finally storing the atmospheric CO 2 from the atmosphere into soil and underground water, are the most main CO 2 carbon sink mode, achieve the purpose of increasing carbon sink, and provide technological support for national carburetion sink and realizing important targets of carbon peak and carbon neutralization.|[0029] In the description of the present specification, the descriptions of the terms "one embodiment," "example," "specific example," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.|[0030] The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof. (CN115445393)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of increasing carbon sink and improving carbon circulation, and particularly relates to a method for improving carbon sink efficiency of soil and underground water.|BACKGROUND ART|[0002] The aim of China is to realize the aims of carbon reaching peak and carbon neutralization in 2030 and 2060 respectively, and increasing the carbon yield and reducing the carbon emission are the most urgent means for realizing the two aims. However, under the current international economic pressure, the promotion of emission reduction work has certain difficulty in order to ensure good development of economy. Thus, adding carbon sinks or finding new ways of carbon sinks is an important ring to achieve both goals. Carbon sequestration is a mechanism for removing CO 2 from the atmosphere, i.e., absorbing CO 2 from the atmosphere into ecosystems such as land and sea and storing it. Wherein, the soil and the groundwater can form the atmospheric CO 2 into dissolved inorganic carbon (mainly comprising several forms, namely dissolved CO 2(aq)、HCO3- ions and CO 32- ions) through the karst action of rock and the hydrolytic action of CO 2 and water. The part of the formed dissolved inorganic carbon mainly enters soil and underground space through a rainfall infiltration channel under the action of rainfall infiltration flushing and is stored to form a carbon sink process for reducing atmospheric CO 2. In this process, two steps are particularly important, namely, the absorption of CO 2 by the soil, and the surface soil has larger pores and can absorb and store atmospheric CO 2. But the soil has different properties, and the porosity and the adsorption capacity are different; secondly, if CO 2 adsorbed and stored by soil does not enter the deep underground space or enters the dynamic underground water space in time, the CO 2 returns to the atmosphere again, carbon sinks cannot be formed, and the main driving force of the process is leaching effect of rainfall infiltration, namely the amount of the rainfall infiltration into the underground water needs to be increased, so that the amount of the CO 2 entering the deep underground space can be increased more, and more carbon sinks are formed.|[0003] Therefore, the method for improving the carbon sink efficiency of the soil and the underground water is developed to perfect the engineering technology of carbon sink improvement in China and improve the practical application prospect of the carbon sink.|DISCLOSURE|Disclosure of Invention|[0004] The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.|[0005] In order to solve the technical problems, the invention is realized by the following technical scheme:|[0006] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps: |[0007] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; |[0008] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 45% -55%; |[0009] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; |[0010] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. |[0011] Preferably, the main rainfall infiltration replenishment area in the first step is used as a rainfall surface runoff collection area, and the rainfall surface runoff collection area comprises a gully and a depression formed by rainfall.|[0012] Preferably, the step of spreading peat soil in the second step specifically includes the following steps: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.|[0013] Preferably, the inserting holes on the tiled peat soil in the third step specifically include the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.|[0014] Preferably, the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions.|[0015] Preferably, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other of which is atmospheric CO 2 absorbed by the soil.|[0016] The invention has the following beneficial effects:|[0017] According to the invention, the content of dissolved inorganic carbon entering the soil and underground water can be greatly increased through the carrying process of soil adsorption and rainfall infiltration leaching, so that atmospheric CO 2 is stored in a deep underground space, the carbon sink efficiency of the soil and underground water is improved, the method has important carbon sink significance, the efficient removal of CO 2 in the atmosphere can be realized, and the environmental negative effect can not be generated. |[0018] Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.|INVENTION MODE|Detailed Description|[0019] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0020] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:|[0021] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; |[0022] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 50%; |[0023] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; |[0024] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. |[0025] According to statistical analysis, the higher the adsorption performance of the soil is, the stronger the adsorption capacity of the soil to atmospheric CO 2 is; in addition, the more rainfall infiltration channels of the soil are, the stronger the rainfall infiltration capacity is, and the more CO 2 is carried by rainfall infiltration, so that the content of dissolved inorganic carbon entering a water body can be effectively increased by 2-3 times by a method of increasing the adsorption quantity of CO 2 in the soil and the rainfall infiltration quantity, and the formed carbon sink quantity is increased by 2-3 times, thereby having important carbon sink economic prospects.|[0026] In this example, the Dissolved Inorganic Carbon (DIC) includes dissolved CO 2、HCO3- ions and CO 32- ions.|[0027] In this embodiment, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other is atmospheric CO 2 absorbed by the soil.|[0028] Increasing the dissolution into the soil and the groundwater is fundamental key to increasing carbon sequestration. While there are two sources of Dissolved Inorganic Carbon (DIC) in soil and groundwater, the highly adsorptive absorption of atmospheric CO 2 by peat soil and the infiltration leaching of atmospheric rainfall carry the absorbed dissolved inorganic carbon. The two parts realize the purposes of reducing, transferring and finally storing the atmospheric CO 2 from the atmosphere into soil and underground water, are the most main CO 2 carbon sink mode, achieve the purpose of increasing carbon sink, and provide technological support for national carburetion sink and realizing important targets of carbon peak and carbon neutralization.|[0029] In the description of the present specification, the descriptions of the terms "one embodiment," "example," "specific example," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.|[0030] The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof. Family Number|(100174807)|100174807|Abstract|(CN114522512 A)|The invention discloses a method for increasing the carbon sink amount of aquatic products , and relates to the technical field of carbon sink increasing and carbon cycle improving . The method comprises the following steps : step 1, absorbing atmospheric CO2 in a carbonate rock weathering process , so that CO2 is temporarily captured and stored in soil pores , and enrichment of CO2 in soil is realized ; step 2, by guiding rainwater in the field area during rainfall , rainwater carrying dissolved inorganic carbon is increased to infiltrate into underground water and flows into a surface water body through surface runoff , and the amount of the dissolved inorganic carbon in the surface water body is increased ; and 3, converting dissolved inorganic carbon in the water body into organic carbon through photosynthesis of the aquatic plants , and storing the organic carbon , so that the aquatic carbon sink in the water body is realized . According to the method , the content of dissolved inorganic carbon entering a surface water body can be greatly increased , so that the fertilization effect is improved , the amount of carbon sink formed by aquatic photosynthesis is increased , the method has important carbon sink significance , CO2 in the atmosphere can be efficiently removed , and the environmental negative effect cannot be generated . |(CN115445393B B)|The invention discloses a method for improving the carbon sink efficiency of soil and underground water , and relates to the technical field of carbon sink increase and carbon cycle improvement . The method comprises the following steps : step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three - dimensional model , and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount ; step 2, paving peat soil with a high - adsorbability and high - water - content space to the area selected in the step 1, and wetting the dried peat soil with water before paving ; thirdly , holes are formed in the laid peat soil , the permeability of a laid area is enhanced , more earth surface rainfall can enter the soil and underground water space through infiltration , and the CO2 amount adsorbed by the peat soil is increased . Through soil adsorption and rainfall infiltration leaching carrying processes , the content of dissolved inorganic carbon entering the soil and underground water is greatly increased , so that atmospheric CO2 is stored in a deep underground space , the carbon sequestration efficiency of the soil and underground water is improved , and important carbon sequestration significance is achieved . |CPC codes|(CN114522512 A)|B01D - 053/14/75 |(CN115445393B B)|B01D - 053/14/75 |IPC codes|(CN114522512 A)|B01D - 053/14 |(CN115445393B B)|B01D - 053/14 | Environmental technology B01D-053/14/75|C02F-003/32|C02F-2101/10|C02F-2103/001|Y02P-060/20 B01D-053/14/75|C02F-003/32|C02F-2101/10|C02F-2103/001|Y02P-060/20 B01D-053/14|C02F-003/32 B01D-053/14|C02F-003/32 CN119028214|CN117069270 CN119028214 112341928 WHO=Examiner SELF=N CAT=A|CN117069270 107332388 WHO=Examiner SELF=N CAT=A AU2020202329|CN106577116|CN105130001|CN102577688 AU2020202329 91096696 WHO=Examiner SELF=N|CN106577116 75959932 WHO=Examiner SELF=N|CN105130001 71632395 WHO=Examiner SELF=N|CN102577688 7762768 WHO=Examiner SELF=N AU2020202329; CN102577688; CN105130001; CN106577116| GRANTED (CN115445393)|GRANTED|(CN114522512)|LAPSED ALIVE (CN115445393)|ALIVE|(CN114522512)|DEAD (CN115445393)|LEGAL DETAILS FOR CN115445393|Actual or expected expiration date=2042-10-26|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-10-26|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202211317927|Application date=2022-10-26|Standardized application number=2022CN-1317927|Event publication date=2022-12-09|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN115445393|Publication stage code=A|Publication date=2022-12-09|Standardized publication number=CN115445393|Event publication date=2022-12-09|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-12-27|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2024-04-26|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN115445393|Publication stage code=B|Publication date=2024-04-26|Standardized publication number=CN115445393B|Event publication date=2024-04-26|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|(CN114522512)|LEGAL DETAILS FOR CN114522512|Actual or expected expiration date=2022-12-06|Legal state=DEAD|Status=LAPSED|Event publication date=2022-01-21|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210073314|Application date=2022-01-21|Standardized application number=2022CN-0073314|Event publication date=2022-05-24|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114522512|Publication stage code=A|Publication date=2022-05-24|Standardized publication number=CN114522512|Event publication date=2022-05-24|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-06-10|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2022-12-06|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication (CN115445393)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTeP+miV6FakRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=KsolU%252FVsjE2he6%252Fe1BZ8qLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN115445393)|CN|(CN115445393)|CN|(CN114522512)|CN (CN115445393)|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN|(CN115445393)|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN|(CN114522512)|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN (CN115445393)|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308|(CN115445393)|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308|(CN114522512)|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308 |(CN115445393)|CN|(CN114522512)|CN (CN115445393)|NAME=YANG MINGXING|NAME=ZHANG MIN|NAME=YANG WU|NAME=XIE FEI|NAME=YAO DUNTING|NAME=LI WEI|(CN115445393)|NAME=YANG MINGXING, COUNTRY=CN |NAME=ZHANG MIN|NAME=YANG WU|NAME=XIE FEI|NAME=YAO DUNTING|NAME=LI WEI|(CN114522512)|NAME=YANG MINGXING, COUNTRY=CN |NAME=ZHANG MIN|NAME=YANG WU|NAME=XIE FEI 10 1 Titre: (CN115445393)|Method for improving carbon sink efficiency of soil and underground water Résumé: (CN115445393)|The invention discloses a method for improving the carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increase and carbon cycle improvement. The method comprises the following steps: step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three-dimensional model, and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount; step 2, paving peat soil with a high-adsorbability and high-water-content space to the area selected in the step 1, and wetting the dried peat soil with water before paving; thirdly, holes are formed in the laid peat soil, the permeability of a laid area is enhanced, more earth surface rainfall can enter the soil and underground water space through infiltration, and the CO2 amount adsorbed by the peat soil is increased. Through soil adsorption and rainfall infiltration leaching carrying processes, the content of dissolved inorganic carbon entering the soil and underground water is greatly increased, so that atmospheric CO2 is stored in a deep underground space, the carbon sequestration efficiency of the soil and underground water is improved, and important carbon sequestration significance is achieved. 98 Abstract gpt-4o-mini no The method focuses on improving carbon sink efficiency through soil and water management rather than accelerating mineral weathering or CO2 capture via mineral carbonation.
97 CN202510111421 CN202510111421 CN119857479 114291372 CN119857479 A 2025-04-22 [CN119857479] 2025-01-23 2025-01-23 2025-04-22 (CN119857479)|2045-01-23 (CN119857479)|Preparation method and application of metal oxide catalyst with potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide (CN119857479)|The invention discloses a preparation method of a metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide, which is characterized in that a manganese ion solution and potassium permanganate are used as raw materials, ultrapure water is used as a solvent, and the metal oxide catalyst is prepared by a hydrothermal synthesis method. According to the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure, the carbon monoxide removal efficiency of the catalyst can be regulated and controlled by adjusting the powder size, and the optimized catalyst can effectively adsorb carbon monoxide and is used for promoting the catalytic oxidation process of carbon monoxide; the size of the catalyst is controlled by using a crusher and a sieve, and the catalyst has excellent catalytic activity and structural stability, can be used for promoting the removal of carbon monoxide, and also has an effective promotion effect on the removal of other toxic and harmful gases, such as nitric oxide, mercury vapor, VOCs (Volatile Organic Compounds) and the like. HENAN POLYTECHNIC UNIVERSITY (CN119857479)|HENAN POLYTECHNIC UNIVERSITY ([CN]) DAN WEIWEI|XUE YIFAN|QIN BENSHUANG|WU MENGLONG|WANG JIAN|PAN RONGKUN (CN119857479)|DAN WEIWEI|XUE YIFAN|QIN BENSHUANG|WU MENGLONG|WANG JIAN|PAN RONGKUN (CN119857479)|GUO LI;BEIJING LVAN IP AGENCY CO., LTD.|Reg. Nb: 16197 (CN119857479)|The application may be better understood by reference to the following description taken in conjunction with the accompanying drawings.|At present, formaldehyde and carbon monoxide are main indoor air pollution sources, formaldehyde and carbon monoxide have fatal harm to human bodies, formaldehyde is colorless and soluble irritant gas, when the indoor content is 0.1 mg/cubic meter, peculiar smell and uncomfortable feeling are generated, 0.5 mg/cubic meter can stimulate eyes to cause lacrimation, 0.6 mg/cubic meter can cause discomfort or pain in throat, even higher concentration can cause nausea, vomiting, cough, chest distress, asthma and even emphysema, 30 mg/cubic meter can cause death immediately, and long-term contact with low-dose formaldehyde can also cause chronic respiratory diseases, female menstrual disorder and pregnancy syndrome, cause the reduction of neonatal physique and chromosomal abnormality, and even cause nasopharyngeal carcinoma.| (CN119857479)|1. The preparation method of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide is characterized by taking manganese ion solution and potassium permanganate as raw materials and ultrapure water as a solvent, and performing hydrothermal synthesis.|10. A metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide is used as a component in a dry powder fire extinguisher and is applied to the removal of carbon monoxide in a fire scene; preferably, the method can also be applied to the removal of other toxic and harmful gases, wherein the harmful gases comprise nitric oxide, mercury vapor and VOCs. | (CN119857479)|The application discloses a preparation method of a metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide, which is characterized in that manganese ion solution and potassium permanganate are used as raw materials, ultrapure water is used as a solvent, and the preparation is carried out by a hydrothermal synthesis method.|The application provides a preparation method of a metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide, which is characterized in that manganese ion solution and potassium permanganate are used as raw materials, ultrapure water is used as a solvent, and the preparation is carried out by a hydrothermal method.|The application relates to a method for manufacturing a semiconductor device.| (CN119857479)|METAL OXIDE CATALYST(100,27)|CARBON MONOXIDE(100,23)|POTASSIUM MANGANESE OXYGEN(100,21)|MOLECULAR SIEVE STRUCTURE(100,18)|OCTAHEDRAL MOLECULAR SIEVE STRUCTURE(100,18)|REMOVING CARBON MONOXIDE(100,12)|CARBON MONOXIDE REMOVAL(100,11)|NOXIOUS GAS(100,6)|TOXIC GAS(100,5)|TOXIC GAS REMOVAL(100,4)|DRY POWDER FIRE EXTINGUISHER(100,3)|EXTINGUISHING POWDER(100,3)|FIRE SCENE(100,3)|MANGANESE ION SOLUTION(80,9)|COLORLESS IRRITANT(79,1)|NEONATAL PHYSIQUE(77,1)|NEONATAL PHYSIQUE REDUCTION(77,1)|OXYGEN OCTAHEDRAL MOLECULAR SIEVE(74,5)|UNCOMFORTABLE FEELING(71,1)|PREGNANCY SYNDROME(69,1)|PECULIAR SMELL(67,1)|CHEST DISTRESS(65,1)|FEMALE MENSTRUAL DISORDER(62,1)|HYDROTHERMAL SYNTHESIS(58,2)|FATAL HARM(58,1)|SOLUBLE IRRITANT GAS(49,1)|POTASSIUM PERMANGANATE(48,14)|FORMALDEHYDE(47,4)|INDOOR CONTENT(45,1)|CHROMOSOMAL ABNORMALITY(36,1)|CAUSE NASOPHARYNGEAL CARCINOMA(35,1)|LACRIMATION(35,1)|CALCINATION(33,7)|CATALYST OPTIMIZATION(33,2)|CATALYTIC OXIDATION PROMOTER(32,2)|DISCOMFORT(31,1)|DISSOLVING POTASSIUM PERMANGANATE(30,2)|VOMITING(30,1)|ULTRAPURE WATER(28,9)|VOCS(28,4)|PROMOTION(28,2)|CHRONIC RESPIRATORY DISEASE(28,1)|PROMOTING REMOVAL(27,2)|ASTHMA(27,1)|NAUSEA(27,1)|MERCURY VAPOR(25,4)|COUGH(25,1)|THROAT(25,1)|DEATH(24,1)|CATALYST CARBON MONOXIDE REMOVAL(23,2)|EVEN EMPHYSEMA(23,1)|NITRIC OXIDE(21,4)|PAIN(21,1)|REGULATION(20,2)|CRUSHER(19,4)|SIEVING(18,3)|MANGANESE NITRATE SOLUTION(17,4)|LOW DOSE FORMALDEHYDE(17,1)|CATALYTIC ACTIVITY(16,2)|EVEN CAUSE NASOPHARYNGEAL CARCINOMA(16,1)|INDOOR AIR POLLUTION(16,1)|NATURAL GROWTH TEMPERATURE(15,2)|INDOOR AIR POLLUTION SOURCE(15,1)|RAW MATERIAL(13,4)|AIR ATMOSPHERE(13,3)|DRYING TEMPERATURE(13,3)|POWDER SIZE(12,2)|PHOTOCATALYST PURIFYING(12,1)|SEMICONDUCTOR DEVICE MANUFACTURING(12,1)|SOLID LIQUID SEPARATION(10,4)|STRUCTURAL STABILITY(10,2)|HUMAN BODY(10,1)|NONEXCLUSIVE INCLUSION(9,1)|FILTRATION ADSORPTION(8,1)|HARMFUL DECORATION RESIDUE REMOVAL(8,1)|PECULIAR SMELL REMOVAL(8,1)|CALCINING TIME(7,2)|MANGANESE NITRATE MOLAR RATIO(7,2)|NATURAL GROWTH TIME(6,2)|BURNING FUEL(6,1)|CATALYST GROWTH ENVIRONMENT(6,1)|CIRCULATION STABILITY(6,1)|COAL BURNING(6,1)|DISSOLVING MANGANESE ORE(6,1)|LONG TERM CONTACT(6,1)|POTASSIUM PERMANGANATE PROPORTION(6,1)|SOOT FINE DUST PARTICLE(6,1)|TITANIUM DIOXIDE PHOTOCATALYST(6,1)|CRUSHING(5,2)|HEATED CONTAINER(5,2)|MUFFLE FURNACE(5,2)|SOLID CALCINATION(5,2)|STIRRING TIME(5,2)|UNIFORM MIXING(5,2)|CARCINOGENICITY(5,1)|CATALYST CRYSTAL(5,1)|COARSE POWDER(5,1)|DRYING OVEN(5,1)|HAZE REDUCTION(5,1)|POSITIVE PROGRESS(5,1)|TECHNICAL DEFECT(5,1)|ACCIDENT(4,1)|ACTIVITY EVALUATION DIAGRAM(4,1)|ANION(4,1)|BACTERIA(4,1)|BENZOPYRENE(4,1)|CALCINING TEMPERATURE(4,1)|CARBON MONOXIDE CATALYTIC OXIDATION(4,1)| (CN119857479)|1. The preparation method of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide is characterized by taking manganese ion solution and potassium permanganate as raw materials and ultrapure water as a solvent, and performing hydrothermal synthesis.|2. The method for preparing a metal oxide catalyst having a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide according to claim 1, comprising the steps of:| (1) Dissolving potassium permanganate in ultrapure water, adding a manganese ion solution, and stirring; | (2) Stirring, then carrying out natural growth, and carrying out solid-liquid separation; | (3) Calcining, and pulverizing. |3. The method for preparing a metal oxide catalyst having a carbon monoxide-removed potassium-manganese-oxygen octahedral molecular sieve structure according to claim 2, wherein in the step (1), the molar ratio of the manganese ion solution to potassium permanganate is 1 (1.2-2.5), for example 1:1.5.|4. The method for preparing a metal oxide catalyst having a carbon monoxide-removed potassium-manganese-oxygen octahedral molecular sieve structure according to claim 2, wherein in the step (1), the manganese ion solution comprises a manganese nitrate solution.|5. The method for preparing a metal oxide catalyst having a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide according to claim 2, wherein in the step (1), the stirring time is 5 to 8 hours.|6. The method for preparing a metal oxide catalyst with a carbon monoxide-removed potassium-manganese-oxygen octahedral molecular sieve structure according to claim 2, wherein in the step (2), the natural growth time is 10-20 hours, and the natural growth temperature is 100-150 ℃.|7. The method for preparing a metal oxide catalyst with a carbon monoxide-removed potassium-manganese-oxygen octahedral molecular sieve structure according to claim 2, wherein in the step (2), drying is further included after solid-liquid separation, and the drying temperature is 80-120 ℃.|8. The method for preparing a metal oxide catalyst having a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide according to claim 2, wherein in the step (3), the calcination is performed at a temperature of 400 to 600 ℃, the calcination time is 4 to 6 hours, and the calcination is performed in an air atmosphere.|9. A metal oxide catalyst having a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide, which is produced by the production method according to any one of claims 1 to 8.|10. A metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide is used as a component in a dry powder fire extinguisher and is applied to the removal of carbon monoxide in a fire scene;| preferably, the method can also be applied to the removal of other toxic and harmful gases, wherein the harmful gases comprise nitric oxide, mercury vapor and VOCs. (CN119857479)|TECHNICAL FIELD|Technical Field|[0001] The application belongs to the technical field of carbon monoxide removal of metal oxide catalysts, and particularly relates to a preparation method and application of a metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for carbon monoxide removal.|BACKGROUND ART|[0002] The air purification is an integral solution for providing sterilization, disinfection, dust and haze reduction, harmful decoration residue removal, peculiar smell removal and the like for various indoor environmental problems, improves living and office conditions, and improves physical and mental health. At present, formaldehyde and carbon monoxide are main indoor air pollution sources, formaldehyde and carbon monoxide have fatal harm to human bodies, formaldehyde is colorless and soluble irritant gas, when the indoor content is 0.1 mg/cubic meter, peculiar smell and uncomfortable feeling are generated, 0.5 mg/cubic meter can stimulate eyes to cause lacrimation, 0.6 mg/cubic meter can cause discomfort or pain in throat, even higher concentration can cause nausea, vomiting, cough, chest distress, asthma and even emphysema, 30 mg/cubic meter can cause death immediately, and long-term contact with low-dose formaldehyde can also cause chronic respiratory diseases, female menstrual disorder and pregnancy syndrome, cause the reduction of neonatal physique and chromosomal abnormality, and even cause nasopharyngeal carcinoma. Pipeline gas is basically popularized in many cities, and the rest uses liquefied petroleum gas. Although liquefied petroleum gas reduces sulfur and dust in coal burning, its main component is hydrocarbon such as propane, and poisoning accident can occur when improper use. When the fuel burns, the oxygen in the room is consumed to discharge toxic gases and particles such as carbon monoxide, carbon dioxide, sulfur dioxide, oxynitride, aldehydes, benzopyrene, soot fine dust particles and the like, which are irritative to nervous systems, conjunctiva and respiratory mucosa and have potential carcinogenicity.|[0003] The existing air purifiers in the market are divided into anion type, ozone type, filtration adsorption type, electrostatic integrated type and photocatalyst type, wherein the photocatalyst type air purifier is a common air purifier, the photocatalyst type air purifier is developed by taking high-efficiency photocatalytic nano titanium dioxide as a raw material, electrons (e-I) carried by a lamp source laser offer are transited to a conduction band by sunlight, ultraviolet light and a fluorescent lamp, corresponding holes (h+) are generated on a valence band, so that oxyhydrogen free radicals, super-oxygen hydroxyl free radicals and super-oxygen ion free radicals with extremely strong oxidation effect are generated, formaldehyde, benzene, toluene, xylene, ammonia, TVOC and other harmful organic matters, pollutants, odor, bacteria, viruses and the like are oxidized and decomposed into harmless CO 2 and H 2 O, but the photocatalyst is required to act under the condition of light, and the purifying efficiency of the nano titanium dioxide photocatalyst on carbon monoxide is low, so that the purifying efficiency of the photocatalyst on indoor air is low.|DISCLOSURE|Disclosure of Invention|[0004] The application aims to overcome the technical defects in the prior art and provide the novel optical fiber. The application relates to a method for manufacturing a semiconductor device.|[0005] The application adopts the following technical scheme to solve the technical problems:|[0006] The application provides a preparation method of a metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide, which is characterized in that manganese ion solution and potassium permanganate are used as raw materials, ultrapure water is used as a solvent, and the preparation is carried out by a hydrothermal method. |[0007] Preferably, the preparation method of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide specifically comprises the following steps:|[0008] (1) Dissolving potassium permanganate in ultrapure water, adding a manganese ion solution, and stirring; |[0009] (2) Stirring, then carrying out natural growth, and carrying out solid-liquid separation; |[0010] (3) Calcining, and pulverizing. |[0011] Preferably, in the step (1), the molar ratio of the manganese ion solution to the potassium permanganate is 1 (1.2-2.5), for example, 1:1.5.|[0012] Wherein, the proportion of potassium permanganate is higher than that of manganese solution in the preparation process.|[0013] Preferably, in step (1), the manganese ion solution comprises a manganese nitrate solution.|[0014] Wherein, the manganese-containing solution can be replaced by a solution containing manganese element or a solution prepared by dissolving manganese ore and nitric acid.|[0015] Preferably, in the step (1), the stirring time is 5-8 hours.|[0016] Preferably, in the step (2), the natural growth time is 10-20 hours, and the natural growth temperature is 100-150 ℃.|[0017] The catalyst is transferred to an oven at 100-150 ℃ in the preparation process of natural growth, and a proper growth reaction environment of catalyst crystals in a solution is provided for the catalyst.|[0018] Preferably, in the step (2), drying is further included after the solid-liquid separation, and the drying temperature is 80-120 ℃.|[0019] The drying temperature is also a proper temperature, so that the drying degree is kept before the solid is calcined in order to ensure that the moisture in the solid is removed, the safety of the subsequent calcination process is ensured, and the quality of the catalyst is not influenced by the moisture.|[0020] Preferably, in the step (3), the calcination temperature is 400-600 ℃, the calcination time is 4-6 hours, and the calcination is performed in an air atmosphere.|[0021] A metal oxide catalyst with a carbon monoxide removal potassium-manganese-oxygen octahedral molecular sieve structure is prepared by the preparation method of the metal oxide catalyst with the carbon monoxide removal potassium-manganese-oxygen octahedral molecular sieve structure.|[0022] A metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide is used as a component in a dry powder fire extinguisher and is applied to the removal of carbon monoxide in a fire scene.|[0023] Preferably, the method can also be applied to the removal of other toxic and harmful gases, wherein the harmful gases comprise nitric oxide, mercury vapor and VOCs.|[0024] Wherein, the screening can be carried out according to the required size in the catalyst preparation process. The catalyst after sieving may be powder, including but not limited to fine powder of 1-100 microns, coarse powder of 100-1000 microns, as desired. The catalyst is fine enough in size and can be made into a dry powder fire extinguisher for removing carbon monoxide in a fire scene. On the basis of conforming to the common knowledge in the field, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the application.|[0025] The reagents and materials used in the present application are commercially available.|[0026] The application has the positive progress effects that:|[0027] the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure is adjusted, the powder size can realize the regulation and control of the carbon monoxide removal efficiency of the catalyst, and the optimized catalyst can effectively adsorb carbon monoxide for promoting the catalytic oxidation process of carbon monoxide. |[0028] The application influences the microstructure of the catalyst and the catalytic oxidation efficiency of carbon monoxide by changing the growth environment of the catalyst, and controls the size of the catalyst by using a crusher and sieving in the process of treating the catalyst, so that the catalyst has excellent catalytic activity and structural stability, which is different from the reported scheme of the catalyst structure so as to promote the carbon monoxide adsorption catalytic oxidation process, and the factors of cost improvement caused by no additional introduction of ligand and poor circulation stability caused by unstable ligand structure are avoided. The application can be used for promoting the removal of carbon monoxide, and has effective promotion effect on the removal of other toxic and harmful gases, such as nitric oxide, mercury vapor, VOCs and the like.|DRAWINGS DESCRIPTION|[0029] The application may be better understood by reference to the following description taken in conjunction with the accompanying drawings. The accompanying drawings, which are included to provide a further illustration of the preferred embodiments of the application and together with a further understanding of the principles and advantages of the application, are incorporated in and constitute a part of this specification.|[0030] Wherein:|[0031] FIG. 1 is a preparation flow chart; |[0032] FIG. 2 is a diagram of a crystal structure; |[0033] FIG. 3 is a diagram of an activity evaluation apparatus; |[0034] FIG. 4 is a graph of carbon monoxide removal efficiency at various temperatures in an N 2-O2 atmosphere. |INVENTION MODE|Detailed Description|[0035] The application is further illustrated by means of the following examples, which are not intended to limit the scope of the application. The experimental methods, in which specific conditions are not noted in the following examples, were selected according to conventional methods and conditions, or according to the commercial specifications.|[0036] The experimental methods used in the following examples are conventional methods unless otherwise specified.|[0037] The starting materials in the examples below are all commercially available.|[0038] Example 1|[0039] The specific preparation process of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure comprises the following steps:|[0040] Dissolving 2.53g of potassium permanganate in a certain amount of ultrapure water, stirring to fully dissolve the potassium permanganate, adding a manganese nitrate solution to enable the molar ratio of manganese nitrate to potassium permanganate to be 3:2, transferring the mixture into a stirrer to stir for more than 5 hours, transferring the mixture into a heating container after uniform mixing, naturally growing the catalyst for about 10 hours under the condition of 120 ℃, filtering to separate solid and liquid components, fully washing the solid obtained by the reaction by using ultrapure water, transferring the washed solid into a drying box, drying the solid at 100 ℃, placing the solid in a muffle furnace after drying until the solid is dried, calcining and preserving the solid for more than 4 hours under the condition of 450 ℃ in an air atmosphere, and crushing, grinding and screening the calcined solid by a crusher to obtain 3.48g of granular potassium-manganese-oxygen octahedral molecular sieve structured metal oxide catalyst. |[0041] Example 2|[0042] The specific preparation process of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure comprises the following steps:|[0043] Dissolving 2.72g of potassium permanganate in a certain amount of ultrapure water, stirring to fully dissolve the potassium permanganate, adding a manganese nitrate solution to enable the molar ratio of manganese nitrate to potassium permanganate to be approximately 4:2, transferring the mixture into a stirrer to stir for more than 5 hours, transferring the mixture into a heating container after uniform mixing, naturally growing the catalyst for about 10 hours under the condition of 150 ℃, filtering to separate solid and liquid components, fully washing the reacted solid by using ultrapure water, transferring the washed solid into a drying oven, drying the solid at the temperature of 80 ℃, placing the solid into a muffle furnace after drying is finished, calcining and preserving the heat for more than 4 hours under the condition of 450 ℃, and crushing, grinding and screening the calcined solid by a crusher to obtain 3.52g of granular metal oxide catalyst of a potassium-manganese-oxygen octahedral molecular sieve structure with uniform size. |[0044] Effect example 1|[0045] The preparation flow chart is shown in fig. 1, the crystal structure chart is shown in fig. 2, and the test device chart of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure is shown in fig. 3.|[0046] The carbon monoxide removal experiment of the prepared metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure in the N 2-O2 atmosphere at different temperatures is shown in the result of FIG. 4.|[0047] As can be seen from the results of FIG. 4, the product prepared in example 1 of the present application has a carbon monoxide removal efficiency of approximately 100% at 200℃or more and an excellent removal effect.|[0048] Finally, it is also noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.|[0049] While the application has been disclosed by the foregoing description of specific embodiments thereof, it will be appreciated that those skilled in the art may devise various modifications, adaptations, or equivalents of the application within the spirit and scope of the appended claims. Such modifications, improvements, or equivalents are intended to be included within the scope of this application as claimed. (CN119857479)|TECHNICAL FIELD|Technical Field|[0001] The application belongs to the technical field of carbon monoxide removal of metal oxide catalysts, and particularly relates to a preparation method and application of a metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for carbon monoxide removal.|BACKGROUND ART|[0002] The air purification is an integral solution for providing sterilization, disinfection, dust and haze reduction, harmful decoration residue removal, peculiar smell removal and the like for various indoor environmental problems, improves living and office conditions, and improves physical and mental health. At present, formaldehyde and carbon monoxide are main indoor air pollution sources, formaldehyde and carbon monoxide have fatal harm to human bodies, formaldehyde is colorless and soluble irritant gas, when the indoor content is 0.1 mg/cubic meter, peculiar smell and uncomfortable feeling are generated, 0.5 mg/cubic meter can stimulate eyes to cause lacrimation, 0.6 mg/cubic meter can cause discomfort or pain in throat, even higher concentration can cause nausea, vomiting, cough, chest distress, asthma and even emphysema, 30 mg/cubic meter can cause death immediately, and long-term contact with low-dose formaldehyde can also cause chronic respiratory diseases, female menstrual disorder and pregnancy syndrome, cause the reduction of neonatal physique and chromosomal abnormality, and even cause nasopharyngeal carcinoma. Pipeline gas is basically popularized in many cities, and the rest uses liquefied petroleum gas. Although liquefied petroleum gas reduces sulfur and dust in coal burning, its main component is hydrocarbon such as propane, and poisoning accident can occur when improper use. When the fuel burns, the oxygen in the room is consumed to discharge toxic gases and particles such as carbon monoxide, carbon dioxide, sulfur dioxide, oxynitride, aldehydes, benzopyrene, soot fine dust particles and the like, which are irritative to nervous systems, conjunctiva and respiratory mucosa and have potential carcinogenicity.|[0003] The existing air purifiers in the market are divided into anion type, ozone type, filtration adsorption type, electrostatic integrated type and photocatalyst type, wherein the photocatalyst type air purifier is a common air purifier, the photocatalyst type air purifier is developed by taking high-efficiency photocatalytic nano titanium dioxide as a raw material, electrons (e-I) carried by a lamp source laser offer are transited to a conduction band by sunlight, ultraviolet light and a fluorescent lamp, corresponding holes (h+) are generated on a valence band, so that oxyhydrogen free radicals, super-oxygen hydroxyl free radicals and super-oxygen ion free radicals with extremely strong oxidation effect are generated, formaldehyde, benzene, toluene, xylene, ammonia, TVOC and other harmful organic matters, pollutants, odor, bacteria, viruses and the like are oxidized and decomposed into harmless CO 2 and H 2 O, but the photocatalyst is required to act under the condition of light, and the purifying efficiency of the nano titanium dioxide photocatalyst on carbon monoxide is low, so that the purifying efficiency of the photocatalyst on indoor air is low.|DISCLOSURE|Disclosure of Invention|[0004] The application aims to overcome the technical defects in the prior art and provide the novel optical fiber. The application relates to a method for manufacturing a semiconductor device.|[0005] The application adopts the following technical scheme to solve the technical problems:|[0006] The application provides a preparation method of a metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide, which is characterized in that manganese ion solution and potassium permanganate are used as raw materials, ultrapure water is used as a solvent, and the preparation is carried out by a hydrothermal method. |[0007] Preferably, the preparation method of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide specifically comprises the following steps:|[0008] (1) Dissolving potassium permanganate in ultrapure water, adding a manganese ion solution, and stirring; |[0009] (2) Stirring, then carrying out natural growth, and carrying out solid-liquid separation; |[0010] (3) Calcining, and pulverizing. |[0011] Preferably, in the step (1), the molar ratio of the manganese ion solution to the potassium permanganate is 1 (1.2-2.5), for example, 1:1.5.|[0012] Wherein, the proportion of potassium permanganate is higher than that of manganese solution in the preparation process.|[0013] Preferably, in step (1), the manganese ion solution comprises a manganese nitrate solution.|[0014] Wherein, the manganese-containing solution can be replaced by a solution containing manganese element or a solution prepared by dissolving manganese ore and nitric acid.|[0015] Preferably, in the step (1), the stirring time is 5-8 hours.|[0016] Preferably, in the step (2), the natural growth time is 10-20 hours, and the natural growth temperature is 100-150 ℃.|[0017] The catalyst is transferred to an oven at 100-150 ℃ in the preparation process of natural growth, and a proper growth reaction environment of catalyst crystals in a solution is provided for the catalyst.|[0018] Preferably, in the step (2), drying is further included after the solid-liquid separation, and the drying temperature is 80-120 ℃.|[0019] The drying temperature is also a proper temperature, so that the drying degree is kept before the solid is calcined in order to ensure that the moisture in the solid is removed, the safety of the subsequent calcination process is ensured, and the quality of the catalyst is not influenced by the moisture.|[0020] Preferably, in the step (3), the calcination temperature is 400-600 ℃, the calcination time is 4-6 hours, and the calcination is performed in an air atmosphere.|[0021] A metal oxide catalyst with a carbon monoxide removal potassium-manganese-oxygen octahedral molecular sieve structure is prepared by the preparation method of the metal oxide catalyst with the carbon monoxide removal potassium-manganese-oxygen octahedral molecular sieve structure.|[0022] A metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide is used as a component in a dry powder fire extinguisher and is applied to the removal of carbon monoxide in a fire scene.|[0023] Preferably, the method can also be applied to the removal of other toxic and harmful gases, wherein the harmful gases comprise nitric oxide, mercury vapor and VOCs.|[0024] Wherein, the screening can be carried out according to the required size in the catalyst preparation process. The catalyst after sieving may be powder, including but not limited to fine powder of 1-100 microns, coarse powder of 100-1000 microns, as desired. The catalyst is fine enough in size and can be made into a dry powder fire extinguisher for removing carbon monoxide in a fire scene. On the basis of conforming to the common knowledge in the field, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the application.|[0025] The reagents and materials used in the present application are commercially available.|[0026] The application has the positive progress effects that:|[0027] the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure is adjusted, the powder size can realize the regulation and control of the carbon monoxide removal efficiency of the catalyst, and the optimized catalyst can effectively adsorb carbon monoxide for promoting the catalytic oxidation process of carbon monoxide. |[0028] The application influences the microstructure of the catalyst and the catalytic oxidation efficiency of carbon monoxide by changing the growth environment of the catalyst, and controls the size of the catalyst by using a crusher and sieving in the process of treating the catalyst, so that the catalyst has excellent catalytic activity and structural stability, which is different from the reported scheme of the catalyst structure so as to promote the carbon monoxide adsorption catalytic oxidation process, and the factors of cost improvement caused by no additional introduction of ligand and poor circulation stability caused by unstable ligand structure are avoided. The application can be used for promoting the removal of carbon monoxide, and has effective promotion effect on the removal of other toxic and harmful gases, such as nitric oxide, mercury vapor, VOCs and the like.|DRAWINGS DESCRIPTION|[0029] The application may be better understood by reference to the following description taken in conjunction with the accompanying drawings. The accompanying drawings, which are included to provide a further illustration of the preferred embodiments of the application and together with a further understanding of the principles and advantages of the application, are incorporated in and constitute a part of this specification.|[0030] Wherein:|[0031] FIG. 1 is a preparation flow chart; |[0032] FIG. 2 is a diagram of a crystal structure; |[0033] FIG. 3 is a diagram of an activity evaluation apparatus; |[0034] FIG. 4 is a graph of carbon monoxide removal efficiency at various temperatures in an N 2-O2 atmosphere. |INVENTION MODE|Detailed Description|[0035] The application is further illustrated by means of the following examples, which are not intended to limit the scope of the application. The experimental methods, in which specific conditions are not noted in the following examples, were selected according to conventional methods and conditions, or according to the commercial specifications.|[0036] The experimental methods used in the following examples are conventional methods unless otherwise specified.|[0037] The starting materials in the examples below are all commercially available.|[0038] Example 1|[0039] The specific preparation process of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure comprises the following steps:|[0040] Dissolving 2.53g of potassium permanganate in a certain amount of ultrapure water, stirring to fully dissolve the potassium permanganate, adding a manganese nitrate solution to enable the molar ratio of manganese nitrate to potassium permanganate to be 3:2, transferring the mixture into a stirrer to stir for more than 5 hours, transferring the mixture into a heating container after uniform mixing, naturally growing the catalyst for about 10 hours under the condition of 120 ℃, filtering to separate solid and liquid components, fully washing the solid obtained by the reaction by using ultrapure water, transferring the washed solid into a drying box, drying the solid at 100 ℃, placing the solid in a muffle furnace after drying until the solid is dried, calcining and preserving the solid for more than 4 hours under the condition of 450 ℃ in an air atmosphere, and crushing, grinding and screening the calcined solid by a crusher to obtain 3.48g of granular potassium-manganese-oxygen octahedral molecular sieve structured metal oxide catalyst. |[0041] Example 2|[0042] The specific preparation process of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure comprises the following steps:|[0043] Dissolving 2.72g of potassium permanganate in a certain amount of ultrapure water, stirring to fully dissolve the potassium permanganate, adding a manganese nitrate solution to enable the molar ratio of manganese nitrate to potassium permanganate to be approximately 4:2, transferring the mixture into a stirrer to stir for more than 5 hours, transferring the mixture into a heating container after uniform mixing, naturally growing the catalyst for about 10 hours under the condition of 150 ℃, filtering to separate solid and liquid components, fully washing the reacted solid by using ultrapure water, transferring the washed solid into a drying oven, drying the solid at the temperature of 80 ℃, placing the solid into a muffle furnace after drying is finished, calcining and preserving the heat for more than 4 hours under the condition of 450 ℃, and crushing, grinding and screening the calcined solid by a crusher to obtain 3.52g of granular metal oxide catalyst of a potassium-manganese-oxygen octahedral molecular sieve structure with uniform size. |[0044] Effect example 1|[0045] The preparation flow chart is shown in fig. 1, the crystal structure chart is shown in fig. 2, and the test device chart of the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure is shown in fig. 3.|[0046] The carbon monoxide removal experiment of the prepared metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure in the N 2-O2 atmosphere at different temperatures is shown in the result of FIG. 4.|[0047] As can be seen from the results of FIG. 4, the product prepared in example 1 of the present application has a carbon monoxide removal efficiency of approximately 100% at 200℃or more and an excellent removal effect.|[0048] Finally, it is also noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.|[0049] While the application has been disclosed by the foregoing description of specific embodiments thereof, it will be appreciated that those skilled in the art may devise various modifications, adaptations, or equivalents of the application within the spirit and scope of the appended claims. Such modifications, improvements, or equivalents are intended to be included within the scope of this application as claimed. Family Number|(114291372)|114291372|Abstract|(CN119857479 A)|The invention discloses a preparation method of a metal oxide catalyst with a potassium - manganese - oxygen octahedral molecular sieve structure for removing carbon monoxide , which is characterized in that a manganese ion solution and potassium permanganate are used as raw materials , ultrapure water is used as a solvent , and the metal oxide catalyst is prepared by a hydrothermal synthesis method . According to the metal oxide catalyst with the potassium - manganese - oxygen octahedral molecular sieve structure , the carbon monoxide removal efficiency of the catalyst can be regulated and controlled by adjusting the powder size , and the optimized catalyst can effectively adsorb carbon monoxide and is used for promoting the catalytic oxidation process of carbon monoxide ; the size of the catalyst is controlled by using a crusher and a sieve , and the catalyst has excellent catalytic activity and structural stability , can be used for promoting the removal of carbon monoxide , and also has an effective promotion effect on the removal of other toxic and harmful gases , such as nitric oxide , mercury vapor , VOCs ( Volatile Organic Compounds ) and the like . |CPC codes|(CN119857479 A)|B01D - 053/86/28 |B01D - 053/86/4 |B01D - 053/86/65 |B01D - 053/86/87 |B01D - 2255/2022 |B01D - 2255/2073 |B01D - 2257/404 |B01D - 2257/502 |B01D - 2257/602 |B01D - 2257/708 |B01J - 023/34 |B01J - 037/08 |B01J - 037/10 |IPC codes|(CN119857479 A)|B01D - 053/44 |B01D - 053/56 |B01D - 053/62 |B01D - 053/64 |B01D - 053/86 |B01J - 023/34 |B01J - 037/08 |B01J - 037/10 | Chemical engineering|Environmental technology B01D-053/86/28|B01D-053/86/4|B01D-053/86/65|B01D-053/86/87|B01D-2255/2022|B01D-2255/2073|B01D-2257/404|B01D-2257/502|B01D-2257/602|B01D-2257/708|B01J-023/34|B01J-037/08|B01J-037/10|Y02A-050/20 B01D-053/86/28|B01D-053/86/4|B01D-053/86/65|B01D-053/86/87|B01D-2255/2022|B01D-2255/2073|B01D-2257/404|B01D-2257/502|B01D-2257/602|B01D-2257/708|B01J-023/34|B01J-037/08|B01J-037/10|Y02A-050/20 B01D-053/44|B01D-053/56|B01D-053/62|B01D-053/64|B01D-053/86|B01J-023/34|B01J-037/08|B01J-037/10 B01D-053/44|B01D-053/56|B01D-053/62|B01D-053/64|B01D-053/86|B01J-023/34|B01J-037/08|B01J-037/10 PENDING (CN119857479)|PENDING ALIVE (CN119857479)|ALIVE (CN119857479)|LEGAL DETAILS FOR CN119857479|Actual or expected expiration date=2045-01-23|Legal state=ALIVE|Status=PENDING|Event publication date=2025-01-23|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510111421|Application date=2025-01-23|Standardized application number=2025CN-0111421|Event publication date=2025-04-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119857479|Publication stage code=A|Publication date=2025-04-22|Standardized publication number=CN119857479|Event publication date=2025-04-22|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-05-09|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN119857479)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQx4ckz9N0u2lfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000077237663&ekey=2135&xpn=CN119857479&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=MEKJS%252B58f5aSSYrXfrPbMZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN119857479)|CN (CN119857479)|NAME=HENAN POLYTECHNIC UNIVERSITY , COUNTRY=CN (CN119857479)|NAME=GUO LI;BEIJING LVAN IP AGENCY CO., LTD. , REG=16197 (CN119857479)|NAME=DAN WEIWEI|NAME=XUE YIFAN|NAME=QIN BENSHUANG|NAME=WU MENGLONG|NAME=WANG JIAN|NAME=PAN RONGKUN 0 1 Titre: (CN119857479)|Preparation method and application of metal oxide catalyst with potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide Résumé: (CN119857479)|The invention discloses a preparation method of a metal oxide catalyst with a potassium-manganese-oxygen octahedral molecular sieve structure for removing carbon monoxide, which is characterized in that a manganese ion solution and potassium permanganate are used as raw materials, ultrapure water is used as a solvent, and the metal oxide catalyst is prepared by a hydrothermal synthesis method. According to the metal oxide catalyst with the potassium-manganese-oxygen octahedral molecular sieve structure, the carbon monoxide removal efficiency of the catalyst can be regulated and controlled by adjusting the powder size, and the optimized catalyst can effectively adsorb carbon monoxide and is used for promoting the catalytic oxidation process of carbon monoxide; the size of the catalyst is controlled by using a crusher and a sieve, and the catalyst has excellent catalytic activity and structural stability, can be used for promoting the removal of carbon monoxide, and also has an effective promotion effect on the removal of other toxic and harmful gases, such as nitric oxide, mercury vapor, VOCs (Volatile Organic Compounds) and the like. 96 Abstract gpt-4o-mini no The article focuses on a metal oxide catalyst for removing carbon monoxide, which does not relate to accelerated weathering or CO₂ capture.
98 CN202510700986 CN202510700986 CN120479411 115651952 CN120479411 A 2025-08-15 [CN120479411] 2025-05-28 2025-05-28 2025-08-15 (CN120479411)|2045-05-28 (CN120479411)|Chromium-modified alumina carrier and preparation method and application thereof (CN120479411)|The invention provides a chromium-modified alumina carrier and a preparation method and application thereof. The preparation method of the chromium modified alumina carrier comprises the following steps: crushing a waste chromium propane dehydrogenation catalyst, carrying out acid leaching, and filtering to obtain an acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues; adding a reducing agent into the filtrate, supplementing aluminum sulfate, and adjusting the pH value of the solution to obtain an acidic solution containing chromium aluminum sulfate; carrying out alkali dissolution on the aluminum oxide filter residues by using alkali liquor to obtain an alkali solution containing sodium metaaluminate; mixing the acidic solution and the alkaline solution, carrying out neutralization reaction, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder; and kneading, extruding, drying and roasting the powder and a forming aid to obtain the chromium-modified alumina carrier. According to the present invention, the waste-free complete utilization of the waste chromium propane dehydrogenation catalyst and the preparation of the chromium modified alumina carrier are achieved, and the prepared carrier can be used for preparing the residual oil hydrogenation carbon residue removal catalyst, such that the carbon residue removal rate can be easily improved, and the carbon deposition generation can be easily reduced. REZEL ENGINEERING (CN120479411)|REZEL ENGINEERING CORP. ([CN]) ZHU WEI|YANG CHENGGONG|SHI ZONGBO|ZHUO RUNSHENG (CN120479411)|ZHU WEI|YANG CHENGGONG|SHI ZONGBO|ZHUO RUNSHENG (CN120479411)|ZHANG JUJIAN;CHENGDU HUAFENG PATENT OFFICE|Reg. Nb: 51223 (CN120479411)|Aiming at the problems that the prior recovery technology still has low metal recovery rate, complex process flow, secondary pollution generation and the like, and the performance cannot meet the requirements, the invention provides a chromium modified alumina carrier and a preparation method and application thereof.|However, the waste catalyst raw material is also stored in the charcoal burning process, the catalyst carbon deposit can be spontaneous-burned and generate open fire at 400-600 ℃, the high-temperature combustion is easy to cause the temperature of a material layer to fly, the temperature control is difficult, the charcoal is burned under the condition of the roasting temperature of 700-950 ℃, the molybdenum trioxide can be sublimated, and the molybdenum recovery rate is reduced.|The catalyst pore canal for removing carbon residue is relatively smaller, generally only tens or tens of nanometers, the diffusion resistance of the macromolecule in the reaction residue to the catalyst pore canal is relatively larger, carbon deposit is deposited on the outer side of the catalyst more, the pore diameter is further reduced, the inner diffusion control effect is more obvious, the macromolecule is more difficult to enter the inside of the catalyst pore canal and is continuously coked at the edge of the catalyst, the utilization rate of active sites in the catalyst pore canal is continuously reduced, and the catalyst deactivation is accelerated.| (CN120479411)|1. The preparation method of the chromium modified alumina carrier is characterized by comprising the following steps: S1, crushing, acid leaching and filtering a waste chromium propane dehydrogenation catalyst to obtain acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues, wherein chromium elements in the acid leaching filtrate containing chromium aluminum sulfate are III and VI; S2, adding a reducing agent into the acid leaching filtrate containing the chromium aluminum sulfate, and reducing VI-valent chromium element in the acid leaching filtrate containing the chromium aluminum sulfate into III-valent chromium element to obtain a solution containing the chromium aluminum sulfate; S3, adding aluminum sulfate into the acid leaching filtrate of the chromium-containing aluminum sulfate according to the chromium and aluminum content of the chromium-modified aluminum oxide carrier, and regulating the pH value by using sulfuric acid and a sodium hydroxide solution to obtain an acidic solution of the chromium-containing aluminum sulfate; S4, alkali liquor is used for dissolving alumina filter residues to obtain an alkaline solution containing sodium metaaluminate; s5, carrying out neutralization precipitation on an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate by adopting a neutralization method, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder; S6, kneading, extruding, drying and roasting the chromium modified aluminum hydroxide powder and the forming auxiliary agent to obtain the chromium modified aluminum oxide carrier. | (CN120479411)|The invention also provides a chromium modified alumina carrier, which is obtained by the preparation method, wherein the specific surface area of the chromium modified alumina carrier is 190-250m 2 /g, and the pore volume is 0.65-0.75mL/g.The invention also provides application of the chromium-modified alumina carrier, and the chromium-modified alumina carrier prepared by the preparation method is applied to residual oil hydrodecarbonization catalysts.|The invention provides a chromium modified alumina carrier, a preparation method and application thereof.|The invention relates to the field of catalyst preparation, in particular to a chromium modified alumina carrier, a preparation method and application thereof.| (CN120479411)|CHROMIUM(100,35)|CHROMIUM MODIFIED ALUMINA CARRIER(100,30)|ALUMINA CARRIER(100,15)|CATALYST PORE CANAL(100,4)|CHROMIUM PROPANE DEHYDROGENIZATION CATALYST(60,14)|DEHYDROGENIZATION CATALYST(56,16)|SODIUM METAALUMINATE(50,23)|ACID LEACHING FILTRATE(47,28)|ALUMINA FILTER RESIDUE(45,13)|NEUTRALIZATION KETTLE(37,14)|CATALYST DEACTIVATION(37,1)|ACIDIC SOLUTION(34,22)|ALKALI LIQUOR(34,5)|CONTAMINATION GENERATION(34,1)|ALKALI DISSOLUTION REACTION(31,10)|CATALYST CARBON(31,1)|DISSOLVING ALUMINA FILTER RESIDUE(30,3)|CHROMIUM ALUMINA FILTER RESIDUE(30,1)|ALKALINE SOLUTION(29,22)|CHROMIUM ACID LEACHING FILTRATE(27,5)|ALUMINUM HYDROXIDE POWDER(26,12)|VI VALENT CHROMIUM(25,9)|SODIUM METAALUMINATE ALKALINE SOLUTION(25,1)|MACROMOLECULE(24,1)|NANOMETER(24,1)|NEUTRALIZING(23,10)|RESIDUAL OIL HYDRODECARBONIZATION CATALYST(23,4)|ROASTING TEMPERATURE(23,3)|DIFFUSION RESISTANCE(23,1)|REACTION RESIDUE(22,1)|III VALENT CHROMIUM(21,6)|REMOVING CARBON RESIDUE(21,1)|CHROMIUM PROPANE(20,14)|CATALYST EDGE(20,1)|CHARCOAL(20,1)|ALUMINUM SULFATE(19,30)|CHROMIUM ALUMINUM SULFATE(18,34)|PORE VOLUME(18,12)|CRUSHED PRODUCT(18,4)|SODIUM HYDROXIDE SOLUTION(17,24)|ACID LEACHING(17,9)|MOLYBDENUM RECOVERY RATE(17,1)|SODIUM HYDROXIDE(16,24)|ALKALI SOLUTION(16,4)|MOLYBDENUM TRIOXIDE(16,2)|ALUMINUM HYDROXIDE(15,13)|CARBON DEPOSITION(15,10)|ALUMINUM OXIDE CARRIER(15,7)|ALUMINUM CONTENT(15,4)|CRUSHING(15,4)|GUAR GUM POWDER(15,4)|PORE DIAMETER(15,2)|KNEADING(14,9)|FULL UTILIZATION(14,2)|CARRIER PREPARATION(14,1)|OPEN FIRE(14,1)|CR CONTENT(13,5)|SULFURIC ACID LEACHING(13,5)|CARBON RESIDUE REMOVAL CATALYST(12,7)|CHARCOAL BURNING(12,1)|SULFURIC ACID(11,37)|CATALYST RESIDUE(10,10)|AUXILIARY AGENT(10,8)|HYDROXYPROPYL CELLULOSE(10,5)|CRUSHED WASTE CATALYST(10,3)|MESH STANDARD(10,3)|ISOVOLUMETRIC IMPREGNATION(10,2)|RESIDUUM HYDRODECARBONIZATION CATALYST EVALUATION(10,1)|WASTE CATALYST RAW MATERIAL(10,1)|REDUCING AGENT(9,16)|ALUMINUM OXIDE(9,10)|SULFURIC ACID SOLUTION(9,7)|EXTRUSION(9,3)|CATALYST FIELD(9,1)|PH VALUE(9,1)|RESIDUUM HYDRODECARBONIZATION CATALYST INDEX(9,1)|BURNED RESIDUE(8,4)|FINISHED CHROMIUM(8,4)|SODIUM BISULFITE(8,4)|SODIUM METABISULFITE(8,4)|AUXILIARY SESBANIA POWDER(8,2)|PRIOR RECOVERY(8,2)|USAGE MASS RATIO(8,2)|CATALYST RAW MATERIAL(8,1)|DOMESTIC PROPANE DEHYDROGENIZATION INDUSTRY(8,1)|PHOSPHOMOLYBDENUM BLUE MICELLE(8,1)|CARBON RESIDUE REMOVAL RATE(7,5)|SODIUM SULFITE(7,5)|HYDROGENATION CARBON RESIDUE(7,3)|HEXAVALENT CHROMIUM PROPORTION(7,2)|RECOVERING MOLYBDENUM(7,2)|WASTE PROPANE DEHYDROGENIZATION CATALYST(7,1)|WET ALUMINA(6,4)|ACTIVE SITE(6,2)|ACTIVE SITE UTILIZATION RATE(6,2)|CLOVER MODULE(6,2)|COMMINUTION EQUIPMENT(6,2)|METAL RECOVERY RATE(6,2)|RECOVERY RATE(6,2)|UTILIZATION RATE(6,2)|CATALYST OUTER SIDE(6,1)|CRUSHED GRANULARITY(6,1)|DIFFUSION CONTROL(6,1)|HYDROTHERMAL CRYSTALIZATION REACTION(6,1)|HYDROTHERMAL CRYSTALIZATION TREATMENT(6,1)|INNER DIFFUSION CONTROL(6,1)|INTERPARTICLE VOID(6,1)|MATERIAL LAYER(6,1)|METALLIC NICKEL DEAROMATIZATION(6,1)|VANADIUM(5,5)|ACID AUXILIARY(5,4)|NEUTRALIZATION TEMPERATURE(5,4)|PREPARED ACIDIC SOLUTION(5,4)|CARRYING OUT NEUTRALIZATION PRECIPITATION(5,3)|SIEVED SAMPLE(5,3)|MASS CONCENTRATION(5,2)|ACTIVATED SPENT CATALYST(5,1)|AIRTIGHT ALKALINE(5,1)|ALUMINA CRYSTALIZATION(5,1)|ALUMINATE SULFATE(5,1)|ATMOSPHERIC RESIDUUM(5,1)|CATALYST ANTICARBON DEPOSITION PERFORMANCE(5,1)|CATALYST DISPERSIVITY(5,1)|CATALYST GRADING(5,1)|HYDROTHERMAL ACTIVATION TREATMENT(5,1)|HYDROTREATING DIFFICULTY(5,1)|III VALENCE CHROMIUM(5,1)|NICKEL VULCANIZATION(5,1)|QUALIFIED IMPURITY CONTENT(5,1)|CITRIC ACID(4,9)|ALUMINA GEL(4,2)|CATALYTIC PERFORMANCE(4,2)|HEAVY OIL HYDROTREATMENT(4,2)|HYDROGENATION CATALYST CARRIER MODIFICATION(4,2)|PORE DISTRIBUTION(4,2)|PRODUCT GRANULARITY(4,2)|ROASTING TIME(4,2)|ALKALI DIGESTION(4,1)|AMORPHOUS ALUMINA CONTENT(4,1)|CARBON DEPOSITION PRECURSOR(4,1)|CARRYING OUT KNEADING(4,1)|CHROMIUM ACCOUNT OXIDE(4,1)|CHROMIUM CATALYST(4,1)|CHROMIUM DISSOLUTION(4,1)|CHROMIUM MODIFIED ALUMINA INDEX(4,1)|CHROMIUM UNIFORM DISPERSION(4,1)|COMPLEXING AUXILIARY AGENT INTRODUCTION(4,1)|HIGH TEMPERATURE COMBUSTION(4,1)|INFRARED ABSORPTION(4,1)|MOLYBDENUM DISTRIBUTION(4,1)|MOLYBDENUM SPECIES(4,1)|OIL ASPHALTENE(4,1)|ONLY TEN(4,1)|OUTER SIDE(4,1)|WEAK ALKALINE HYDROTHERMAL CONDITION(4,1)|MIXED SOLUTION(3,5)|SOLID ALUMINUM SULFATE(3,5)|ICP OE(3,4)|METAL AUXILIARY(3,4)|MODIFIED ALUMINA CARRIER PRODUCTION(3,4)|POWDER FINISHED PRODUCT(3,4)|SOLID CONTENT(3,4)|STANDBY(3,4)|VOLUME RATIO(3,4)|COLLOID(3,2)|COMPLEX PROCESS FLOW(3,2)|CONCENTRATED NITRIC ACID(3,2)|MOLYBDENUM DISULFIDE(3,2)|ACIDIC DISSOLUTION(3,1)|ACTIVITY STABILITY(3,1)|ALKALI DISSOLUTION ALUMINA PRESSURE(3,1)|ALKALI MELTING(3,1)|ALUMINUM HYDROXIDE COPRECIPITATION(3,1)|ALUMINUM RESOURCE(3,1)|CARBON RESIDUE DEEP CONVERSION(3,1)|CARRIER PRECURSOR(3,1)|CATALYST PORE DIAMETER(3,1)|CHROMIUM UNIFORM DISTRIBUTION(3,1)|DEMETALLIZING(3,1)|DENITRIFICATION RATE(3,1)|DESULFURIZATION(3,1)|DISSOLUTION REACTION(3,1)|FIXED BED HYDROGENATION REACTOR(3,1)|HEXAVALENT CHROMIUM CONTENT(3,1)|HOT ALKALI DISSOLUTION(3,1)|HYDROGENATION REACTION(3,1)|INVESTMENT COST(3,1)|MATURE PROCESSING(3,1)|MOLYBDENUM FORMATION(3,1)|NICKEL METAL(3,1)|PERFORMING HYDROGENATION(3,1)|RECOVERY TREATMENT(3,1)|RESIDUAL OIL HYDROGENATION CATALYST(3,1)|RESIDUUM HYDROTREATING(3,1)|RESOURCE RECOVERY DOUBLE TARGET(3,1)|SCREENED SAMPLE(3,1)|SULFUR CONTENT(3,1)|TRACE CARBON RESIDUE CONTENT(3,1)|TUBULAR FURNACE(3,1)|UNIFORM PRECIPITATION(3,1)|ADDITIVE(2,3)|AMMONIUM BICARBONATE SOLUTION(2,1)|ATOMIC ABSORPTION SPECTROPHOTOMETRY(2,1)|AUXILIARY AGENT ACCOUNT(2,1)|BASIC NICKEL CARBONATE(2,1)|BET(2,1)| (CN120479411)|1. The preparation method of the chromium modified alumina carrier is characterized by comprising the following steps:| S1, crushing, acid leaching and filtering a waste chromium propane dehydrogenation catalyst to obtain acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues, wherein chromium elements in the acid leaching filtrate containing chromium aluminum sulfate are III and VI; | S2, adding a reducing agent into the acid leaching filtrate containing the chromium aluminum sulfate, and reducing VI-valent chromium element in the acid leaching filtrate containing the chromium aluminum sulfate into III-valent chromium element to obtain a solution containing the chromium aluminum sulfate; | S3, adding aluminum sulfate into the acid leaching filtrate of the chromium-containing aluminum sulfate according to the chromium and aluminum content of the chromium-modified aluminum oxide carrier, and regulating the pH value by using sulfuric acid and a sodium hydroxide solution to obtain an acidic solution of the chromium-containing aluminum sulfate; | S4, alkali liquor is used for dissolving alumina filter residues to obtain an alkaline solution containing sodium metaaluminate; | s5, carrying out neutralization precipitation on an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate by adopting a neutralization method, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder; | S6, kneading, extruding, drying and roasting the chromium modified aluminum hydroxide powder and the forming auxiliary agent to obtain the chromium modified aluminum oxide carrier. |2. The preparation method of claim 1, wherein the crushed product of the waste chromium-based propane dehydrogenation catalyst has a passing rate of 80 mesh standard sieve of 98% or more.|3. The preparation method according to claim 2, wherein in the sulfuric acid leaching step, the concentration of the sulfuric acid solution is 0.5-1.5mol/L, the temperature of the acid leaching is 40-60 ℃, the time of the acid leaching is 10-30min, and the solid-liquid mass volume ratio of the crushed product of the waste chromium propane dehydrogenation catalyst to the sulfuric acid solution is 1 (10-20) g/mL.|4. The preparation method according to claim 1, wherein in the step S2, the reducing agent comprises one or more of sodium sulfite, sodium bisulphite and sodium metabisulfite, and the mass ratio of the actual usage amount of the reducing agent to the theoretical value is (1.1-1.3): 1, and the reduction time is 20-40min.|5. The preparation method according to claim 1, wherein in the step S3, aluminum sulfate is solid or liquid, and the pH value is adjusted to 3-4 by using sulfuric acid and sodium hydroxide solution, so as to obtain an acidic solution of chromium-containing aluminum sulfate, wherein the concentration of the acidic solution is 100-200g/L calculated by Al 2O3.|6. The preparation method according to claim 1, wherein in the step S4, the alkali solution is sodium hydroxide solution, the mass concentration of the sodium hydroxide solution is 30% -35%, the mass ratio of the sodium hydroxide solution to the alumina filter residue dry basis is 3.3-3.5, the temperature of the alkali dissolution reaction is 100-150 ℃, the time of the alkali dissolution reaction is 2-6h, and the concentration of the alkali solution containing sodium metaaluminate obtained after the alkali dissolution reaction is 150-300g/L calculated by Al 2O3.|7. The preparation method according to claim 1, wherein the neutralization method comprises the steps of adding an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate into a neutralization kettle in parallel, controlling the pH value to be 7-10, reacting for 1-4 hours at 50-80 ℃ in the neutralization kettle, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder, wherein the content of Cr 2O3 is 0.5-3.0%.|8. The preparation method according to claim 1, wherein the forming aid comprises one or more of sesbania powder, citric acid, guar gum powder and hydroxypropyl cellulose;| the roasting temperature is 550-650 ℃, and the roasting time is 2-4h. |9. A chromium-modified alumina carrier, characterized in that the chromium-modified alumina carrier is obtained by the preparation method of any one of claims 1 to 8, the specific surface area of the chromium-modified alumina carrier is 190 to 250m 2/g, and the pore volume is 0.65 to 0.75mL/g.|10. The use of a chromium-modified alumina carrier prepared by the method according to any one of claims 1 to 8 or the chromium-modified alumina carrier according to claim 9 in a residuum hydrodecarbonization catalyst. (CN120479411)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the field of catalyst preparation, in particular to a chromium modified alumina carrier, a preparation method and application thereof.|BACKGROUND ART|[0002] In petroleum refining, oil which remains after vacuum distillation and corresponds to an atmospheric pressure of >500 ℃ is generally called Vacuum Residue (VR), and oil which remains after atmospheric distillation and corresponds to an atmospheric pressure of >350 ℃ is also called Atmospheric Residue (AR). The residual oil has complex composition, large average relative molecular mass, high viscosity, high carbon residue value, and large amount of harmful elements such as metal, sulfur, nitrogen, colloid, asphaltene and the like, and has high hydrotreating difficulty.|[0003] The fixed bed hydrogenation technology is the most mature and fast-growing processing means with the largest devices in the residuum hydrotreating process. The fixed bed hydrogenation adopts a catalyst grading technology, and is respectively filled with a plurality of protective agents (HG), demetallizing agents (HDM), desulfurizing agents (HDS) and carbon residue removing catalysts (HDCCR) according to a proper proportion, and hydrogenation reaction is carried out within a certain temperature range, so that hydrogenation products with qualified impurity contents such as metal, sulfur, nitrogen, carbon residue and the like are obtained.|[0004] With the increasing degradation of the processed raw materials, the carbon residue value of the raw materials is higher and higher, and the load of the carbon residue removal catalyst responsible for the deep conversion of carbon residue is higher and higher. Because the carbon residue removal catalyst is positioned at the tail end of the residual oil hydrogenation catalyst system, compared with other catalysts, the reaction temperature is high, the hydrogen partial pressure is low, and after the hydrogenation of the front-end catalyst, the colloid structure of the oil asphaltene is destroyed, so that the carbon residue removal catalyst Yi Shengjiao has the carbon deposit amount of generally up to 20 percent. The catalyst pore canal for removing carbon residue is relatively smaller, generally only tens or tens of nanometers, the diffusion resistance of the macromolecule in the reaction residue to the catalyst pore canal is relatively larger, carbon deposit is deposited on the outer side of the catalyst more, the pore diameter is further reduced, the inner diffusion control effect is more obvious, the macromolecule is more difficult to enter the inside of the catalyst pore canal and is continuously coked at the edge of the catalyst, the utilization rate of active sites in the catalyst pore canal is continuously reduced, and the catalyst deactivation is accelerated. Therefore, in order to improve the activity stability of the catalyst, researchers have focused on enhancing the anti-carbon deposition performance of the catalyst, improving the distribution of carbon deposition in the radial direction of the catalyst and improving the high temperature stability of the active phase.|[0005] At present, the following strategies are mainly adopted, namely, firstly, the acid strength, the acid quantity and the acid property of a carrier are regulated and controlled, and the generation rate of carbon deposition precursors is reduced, such as K, mg, B, F and the like are added. For example, chinese patent publication No. CN106622264a discloses a hydrodecarbonization catalyst, a preparation method and application thereof, the catalyst comprises an active metal component and a modified hydrogenation catalyst carrier, the modified hydrogenation catalyst carrier comprises a carrier, and a metal auxiliary and an acid auxiliary supported on the carrier, the metal auxiliary and the acid auxiliary are layered on the carrier, the shell layer is the metal auxiliary, the core layer is the acid auxiliary, the metal auxiliary is a group IA metal component and/or a group IIA metal component (e.g., mg, K, ca, etc.), and the acid auxiliary is at least one component selected from F, P and B. The hydrodecarbonization catalyst prepared by the method can obtain higher denitrification rate and carbon residue removal rate in the application of heavy oil hydrotreatment and has lower carbon deposit amount after heavy oil hydrotreatment, so the catalyst has high stability and long service life. Secondly, the number of diffusion holes is properly increased, the carbon deposition capacity is improved, the uniform distribution of carbon deposition in the radial direction of the catalyst is promoted, and the utilization rate of active sites in the holes is improved. For example, chinese patent publication No. CN103785397a discloses a hydrodecarbonization catalyst and a preparation method thereof. The alumina gel treated by high temperature and high pH aging has high crystallinity, less amorphous alumina and relatively larger crystal grains. The reduction of the amorphous alumina content promotes the increase of inter-particle voids, relatively uniform boehmite grain size and promotes the concentration of catalyst pore diameters. The catalyst prepared by uniformly mixing and shaping the alumina gel and the ammonium aluminum carbonate has concentrated pore distribution of 6-10nm and proper pore distribution of more than 100nm, and has low active component content and high carbon residue removal, metal removal and desulfurization activities. Third, the hydrogenation performance of the carrier active phase is improved. Chinese patent publication No. CN114643079a discloses a hydrogenation carbon residue removal catalyst, its preparation method and application. The hydrodecarbonization catalyst is used in the hydrodecarbonization process of heavy oil, can deeply remove polycyclic aromatic hydrocarbon and carbon residue in heavy oil, and has good stability. The molybdenum species form phosphomolybdenum blue micelle protected by the surfactant, so that the distribution of molybdenum in the catalyst is concentrated, and the molybdenum with higher polymerization degree is more favorable for forming high-stacking and long-platelet with improved upper-platelet clusters on the surface of the carrier after vulcanization, thereby obtaining the catalyst with lower intrinsic activation energy and more outstanding low-temperature activity. Meanwhile, as +5 molybdenum in the phosphomolybdenum blue is more easily vulcanized into +4 molybdenum disulfide, the molybdenum formation rate of molybdenum disulfide is increased, and the introduction of the complexing auxiliary agent delays the vulcanization of nickel, so that an active phase structure which takes MoS 2 as a framework and is formed in the catalyst and is formed by high-efficiency hydrogenation and dearomatization of metallic nickel on the outer surface is more easily realized.|[0006] Although the method can improve the performance and prolong the service life of the residual oil hydrodecarbonization catalyst, the method also has the problem of high production cost. The carbon residue removing agent is the variety with the highest active metal content in the residual oil hydrogenation series catalyst, and the price is the highest, so the catalyst is particularly sensitive to cost control. For the carbon residue removal catalyst, the cost of the active metal and the auxiliary agent accounts for about 70-80%, and the cost of the carrier accounts for about 20-30%. In recent years, a route for recovering active metals and alumina and preparing the catalyst by using waste catalysts as raw materials is paid attention to gradually, but the prior recovery technology still has the defects of low metal recovery rate, complex process flow, secondary pollution and the like. For example, chinese patent publication No. CN114602484a discloses a method for preparing a hydrodecarbonization catalyst, in which after the powder of the spent catalyst is decarbonized, ammonium bicarbonate is subjected to hydrothermal activation treatment, on the one hand, active metal molybdenum in the spent catalyst and vanadium deposited in the reaction process undergo dissolution reaction, and on the other hand, alumina in the spent catalyst undergoes hydrothermal crystallization reaction under airtight and weak alkaline hydrothermal conditions, and due to dissolution of metal molybdenum and vanadium and crystallization of alumina, the pore structure of the activated spent catalyst is well improved. The metakaolin is subjected to hydrothermal crystallization treatment by ammonium bicarbonate solution, the specific surface and pore volume are improved, etching points are formed on the surface of metakaolin grains, and the pore channel content of the material is improved by 10-20 nm. The above patents utilize waste catalysts, although achieving the effects of improving catalyst performance and reducing cost. However, the waste catalyst raw material is also stored in the charcoal burning process, the catalyst carbon deposit can be spontaneous-burned and generate open fire at 400-600 ℃, the high-temperature combustion is easy to cause the temperature of a material layer to fly, the temperature control is difficult, the charcoal is burned under the condition of the roasting temperature of 700-950 ℃, the molybdenum trioxide can be sublimated, and the molybdenum recovery rate is reduced.|[0007] Therefore, development of a method capable of preparing a catalyst with excellent performance for carbon residue removal and realizing efficient recycling of resources is needed.|DISCLOSURE|Disclosure of Invention|[0008] Aiming at the problems that the prior recovery technology still has low metal recovery rate, complex process flow, secondary pollution generation and the like, and the performance cannot meet the requirements, the invention provides a chromium modified alumina carrier and a preparation method and application thereof.|[0009] The technical method of the invention is as follows:| the preparation method of the chromium modified alumina carrier comprises the following steps: | S1, crushing, acid leaching and filtering a waste chromium propane dehydrogenation catalyst to obtain acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues, wherein chromium elements in the acid leaching filtrate containing chromium aluminum sulfate are III and VI; | S2, adding a reducing agent into the acid leaching filtrate containing the chromium aluminum sulfate, and reducing VI-valent chromium element in the acid leaching filtrate containing the chromium aluminum sulfate into III-valent chromium element to obtain a solution containing the chromium aluminum sulfate; | S3, adding aluminum sulfate into the acid leaching filtrate of the chromium-containing aluminum sulfate according to the chromium and aluminum content of the chromium-modified aluminum oxide carrier, and regulating the pH value by using sulfuric acid and a sodium hydroxide solution to obtain an acidic solution of the chromium-containing aluminum sulfate; | S4, alkali liquor is used for dissolving alumina filter residues to obtain an alkaline solution containing sodium metaaluminate; | s5, carrying out neutralization precipitation on an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate by adopting a neutralization method, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder; | S6, kneading, extruding, drying and roasting the chromium modified aluminum hydroxide powder and the forming auxiliary agent to obtain the chromium modified aluminum oxide carrier. |[0010] In the step S1, the product granularity of the crushed waste chromium propane dehydrogenation catalyst is 80-mesh standard sieve passing rate which is more than or equal to 98 percent. In the sulfuric acid leaching step, the concentration of the sulfuric acid solution is 0.5-1.5mol/L, the temperature of the acid leaching is 40-60 ℃, the time of the acid leaching is 10-30min, and the solid-liquid mass volume ratio of the crushed product of the waste chromium propane dehydrogenation catalyst to the sulfuric acid solution is 1 (10-20) g/mL. Here, the alumina filter residue is in an aqueous state, and may be optionally washed or not washed, and the alkali dissolution reaction is directly performed without washing by default for simplifying the process.|[0011] In the step S2, the reducing agent comprises one or more of sodium sulfite, sodium bisulfite and sodium metabisulfite, the mass ratio of the actual usage amount of the reducing agent to the theoretical value is (1.1-1.3): 1, and the reduction time is 20-40min.|[0012] In the step S3, aluminum sulfate is solid or liquid, sulfuric acid and sodium hydroxide solution are used for adjusting the pH value of acid leaching filtrate of chromium-containing aluminum sulfate to 3-4, and then the acid solution of chromium-containing aluminum sulfate is obtained, wherein the concentration of the acid solution is 100-200g/L calculated by Al 2O3.|[0013] In the step S4, the alkali liquor is sodium hydroxide solution, the mass concentration of the sodium hydroxide solution is 30% -35%, the mass ratio of the sodium hydroxide solution to the alumina filter residue dry base (without water) is 3.3-3.5, the temperature of the alkali dissolution reaction is 100-150 ℃, the time of the alkali dissolution reaction is 2-6h, and the concentration of the alkali solution containing sodium metaaluminate obtained after the alkali dissolution reaction is 150-300g/L calculated by Al 2O3.|[0014] In the step of S5, the step of the neutralization method comprises the steps of adding an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate into a neutralization kettle in parallel, controlling the pH value to be 7-10, reacting for 1-4 hours at 50-80 ℃ in the neutralization kettle, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder, wherein the content of Cr 2O3 is 0.5-3.0%.|[0015] In the step S6, the forming auxiliary agent comprises one or more of sesbania powder, citric acid, guar gum powder and hydroxypropyl cellulose, the roasting temperature is 550-650 ℃, and the roasting time is 2-4h.|[0016] The invention also provides a chromium modified alumina carrier, which is obtained by the preparation method, wherein the specific surface area of the chromium modified alumina carrier is 190-250m 2/g, and the pore volume is 0.65-0.75mL/g.|[0017] The invention also provides application of the chromium-modified alumina carrier, and the chromium-modified alumina carrier prepared by the preparation method is applied to residual oil hydrodecarbonization catalysts.|[0018] The beneficial effects of the invention are as follows:| 1. The invention provides a preparation method of a chromium modified alumina carrier based on a recovered waste chromium propane dehydrogenation catalyst, which is characterized in that chromium (Cr) and aluminum (Al) resources in a waste agent are efficiently separated and recovered, and a catalyst carrier with a pore structure is reconstructed through a neutralization reaction process. The catalyst carrier with the reconstructed pore structure can realize the uniform dispersion of chromium and obtain the specific surface area, the pore diameter and the pore volume which are suitable for the hydrogenation carbon residue removal catalyst. Specifically, the invention takes waste chromium propane dehydrogenation catalyst as raw materials, based on the main components of chromium oxide, aluminum oxide and chromium element which coexist in III valence and VI valence, firstly, sulfuric acid leaching is adopted to dissolve chromium to form acid leaching filtrate containing chromium aluminum sulfate, and alumina filter residues are produced at the same time, and aiming at the problem that VI valence chromium in the acid leaching filtrate is difficult to be directly precipitated in the subsequent neutralization reaction process, the VI valence chromium is converted into III valence chromium which is easy to precipitate by adding a reducing agent. Then, alkali dissolution reaction is carried out on the alumina filter residues, so that the alumina filter residues are converted into alkaline solution containing sodium metaaluminate. And finally, precisely controlling the pH value of the acid leaching filtrate and the contents of Cr and Al, neutralizing and precipitating the two solutions by a neutralization method, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder, adding a forming auxiliary agent, and then carrying out the processes of kneading, extruding, drying, roasting and the like to prepare the chromium modified aluminum oxide carrier. Through the process, the specific surface area of the carrier finished product reaches 190-250m < 2 >/g through a BET method, the pore volume is 0.65-0.75mL/g, the high-efficiency recovery of chromium and aluminum resources in the waste catalyst is realized, the catalyst prepared by the carrier has higher carbon residue removal rate and less carbon deposit, and the double targets of resource recovery and catalyst performance improvement are achieved. |[0019] 2. The invention realizes the full utilization of the waste chromium propane dehydrogenation catalyst, shortens the treatment process flow, reduces the production cost of the carrier, and simultaneously adopts a neutralization and uniform precipitation method to realize the uniform distribution of chromium element, thereby being beneficial to the improvement of the catalytic performance. The catalyst is applied to the residual oil hydrodecarbonization process, can improve the removal rate of residual oil carbon residue by the catalyst, reduce the carbon deposition generation rate and prolong the service life of the catalyst.|INVENTION MODE|Detailed Description|[0020] The following description of the present invention will be made clearly and fully, and it is apparent that the embodiments described are some, but not all, of the embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0021] The invention is characterized in that the residual oil hydrodecarbonization catalyst has the problems of high-temperature aggregation of active components, reduced activity, coverage of active centers and acid centers by carbon deposit and the like in use. The existing solutions can improve performance, but the production cost is high due to the high cost ratio of active metal and carrier. Based on the method, the active metal of the hydrogenation catalyst is recovered as a key break, the main current technology is a technology for recovering molybdenum, nickel and vanadium by alkali melting or a technology for recovering molybdenum, nickel and vanadium by acid dissolution, and a large amount of aluminum is dissolved out (about 10-20%) in the two technologies, so that the subsequent separation of molybdenum, nickel and vanadium is difficult, the technological process becomes complicated, and the residual carrier for recovering the active metal is difficult to recycle due to irreversible change of pore structure and surface acidity caused by deposited metal and carbon deposition. Meanwhile, the domestic propane dehydrogenation industry is vigorously developed, and a fixed bed Propane Dehydrogenation (PDH) process is favored because of the advantages of simple reactor structure and low investment cost. However, the chromium catalyst (Cr content is generally 5-20wt%, and the rest is alumina and a small amount of auxiliary agent) used by the catalyst is regenerated and used for many times, so that the activity is gradually reduced, and finally the recovery treatment is needed. Therefore, the invention can shorten the process flow, reduce the environmental pollution and recycle valuable metal resources (such as chromium) by recycling the waste chromium propane dehydrogenation catalyst, and avoid the dilemma of recycling the hydrogenation catalyst.|[0022] The invention provides a preparation method of a chromium modified alumina carrier, which comprises the following steps:| S1, crushing, acid leaching and filtering the waste chromium propane dehydrogenation catalyst to obtain acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues, wherein chromium elements in the acid leaching filtrate containing chromium aluminum sulfate are III and VI. |[0023] In one embodiment, comminution employs comminution equipment common in the art. The product granularity of the crushed waste chromium propane dehydrogenation catalyst is 80 mesh standard sieve passing rate more than or equal to 98 percent.|[0024] In one embodiment, the concentration of the sulfuric acid solution in the sulfuric acid leaching step is 0.5-1.5mol/L. For example, the concentration of the sulfuric acid solution may be 0.7mol/L, 1.2mol/L. The temperature of the acid leaching is 40-60 ℃. For example, the temperature may be 45 ℃, 50 ℃. The pickling time is 10-30min. For example, the time may be 15min, 20min. The solid-liquid mass volume ratio of the crushed product of the waste chromium propane dehydrogenation catalyst to the sulfuric acid solution is 1 (10-20) g/mL. For example, the solid-to-liquid ratio is 1:12g/mL, 1:15g/mL.|[0025] Specifically, the equation for sulfuric acid leaching is:|Al2O3+3H2SO4→Al2(SO4)3+3H2O|Cr2O3+3H2SO4→Cr2(SO4)3+3H2O|CrO3+H2O→H2CrO4|2H2CrO4→H2Cr2O7+3H2O| Cr 2O3 (III-valent chromium) is insoluble in water but soluble in sulfuric acid, cr 3+ ions are formed to enter pickle liquor, precipitation is easy to generate when meeting alkali, crO 3 (VI-valent chromium) is soluble in water but exists in a sulfuric acid system in a Cr 2O72-/CrO42- form, precipitation is not easy to generate when meeting alkali, and recovery is realized by reduction and conversion into III-valent chromium. |[0026] S2, adding a reducing agent into the acid leaching filtrate containing the chromium aluminum sulfate, and reducing VI-valent chromium element in the acid leaching filtrate containing the chromium aluminum sulfate into III-valent chromium element to obtain a solution containing the chromium aluminum sulfate.|[0027] In one embodiment, the reducing agent includes one or more of sodium sulfite (Na 2SO3), sodium bisulfite (NaHSO 3), sodium metabisulfite (Na 2S2O5).|[0028] Specifically, the equation for the reduction process is:|H2Cr2O7+3Na2SO3+3H2SO4→Cr2(SO4)3+3Na2SO4+4H2O|2H2Cr2O7+6NaHSO3+3H2SO4→2Cr2(SO4)3+3Na2SO4+8H2O|2H2Cr2O7+3Na2S2O5+3H2SO4→2Cr2(SO4)3+3Na2SO4+5H2O| in one embodiment, the mass ratio of the actual amount of the reducing agent to the theoretical value is (1.1-1.3): 1. The excessive reducing agent ensures that the VI-valent chromium is completely reduced. |[0029] In one embodiment, the reduction time is 20-40 minutes. For example, the temperature of the reduction may be 25min, 30min.|[0030] In the subsequent neutralization precipitation process, acid-base neutralization reaction is needed, and if VI-valent chromium exists, the VI-valent chromium cannot participate in the reaction to generate precipitation, so that the VI-valent chromium is converted into III-valent chromium which is easy to precipitate by adding a reducing agent to generate precipitation, and the VI-valent chromium is prevented from being wasted.|[0031] S3, adding aluminum sulfate into the acid leaching filtrate of the chromium-containing aluminum sulfate according to the chromium and aluminum content of the chromium-modified aluminum oxide carrier, and regulating the pH value by using sulfuric acid and a sodium hydroxide solution to obtain an acidic solution of the chromium-containing aluminum sulfate.|[0032] In one embodiment, the aluminum sulfate is a solid or a liquid, preferably a solid. According to the invention, aluminum sulfate is added according to the chromium and aluminum contents, and the chromium content of the generated aluminum hydroxide powder is regulated and controlled, so that the proportion of chromium in the alumina carrier is regulated, and finally the carbon residue removal performance is optimized.|[0033] In one embodiment, the pH is adjusted to 3-4 using sulfuric acid and sodium hydroxide solution to provide an acidic solution of chromium-containing aluminum sulfate at a concentration of 100-200g/L calculated as Al 2O3.|[0034] S4, alkali liquor is used for dissolving the alumina filter residues, and an alkaline solution containing sodium metaaluminate is obtained.|[0035] In one embodiment, the lye is sodium hydroxide solution. The concentration of the sodium hydroxide solution is 30% -35%. For example, the concentration may be 32%, 34%.|[0036] Specifically, the equation for the alkali dissolution reaction is:|Al2O3+2NaOH→2NaAlO2+H2O| in one embodiment, the mass ratio of sodium hydroxide solution to alumina filter residue dry basis (without water) is 3.3-3.5. For example, the mass ratio may be 3.4. |[0037] In one embodiment, the temperature of the alkali dissolution reaction is 100-150 ℃, the time of the hot alkali dissolution reaction is 2-6h, and the pressure of the alkali dissolution alumina filter residue reaction is normal pressure. For example, the temperature may be 120 ℃, 140 ℃. The time can be 3h or 4h.|[0038] In one embodiment, the alkali solution containing sodium metaaluminate obtained after the alkali dissolution reaction has a concentration of 150-300g/L calculated as Al 2O3.|[0039] S5, carrying out neutralization precipitation on the acidic solution containing chromium aluminum sulfate and the alkaline solution containing sodium metaaluminate by adopting a neutralization method, filtering, washing, drying and crushing to obtain the chromium modified aluminum hydroxide powder.|[0040] In one embodiment, the neutralization method comprises the steps of adding an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate into a neutralization kettle in parallel, controlling the pH value to be 7-10, reacting for 1-4 hours at 50-80 ℃ in the neutralization kettle, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder, wherein the content of Cr 2O3 is 0.5-3.0%. Here, the number of times of washing with water may be 2 or more. Deionized water is used for water washing. The drying can be vacuum drying or natural drying. The comminution is carried out using comminution equipment which is customary in the art. The crushed granularity is 180 mesh standard sieve passing rate >98%.|[0041] In the invention, chromium element exists in an acidic solution containing chromium aluminum sulfate in the form of soluble ions (such as Cr 3+), the solution is acidic, an alkaline solution containing sodium metaaluminate is alkaline, the acidic solution and the alkaline solution are mixed and then undergo a neutralization reaction, and coprecipitation of aluminum hydroxide and chromium hydroxide is formed through acid-base neutralization, so that chromium components are dispersed more uniformly in a carrier precursor, the synergistic effect of a chromium auxiliary agent and an alumina carrier is promoted, and the performance of the chromium auxiliary agent is fully exerted.|[0042] The neutralization method provided by the invention is a short-flow and waste-free method.|[0043] S6, kneading, extruding, drying and roasting the chromium modified aluminum hydroxide powder and the forming auxiliary agent to obtain the chromium modified aluminum oxide carrier.|[0044] In one embodiment, the forming aid comprises one or more of sesbania powder, citric acid, guar gum powder, hydroxypropyl cellulose. Further, the forming aid may also include an acetic acid solution or a nitric acid solution.|[0045] In one embodiment, the kneading step comprises mixing chromium-modified aluminum oxide with one or more of sesbania powder, citric acid, guar gum powder and hydroxypropyl cellulose, and adding acetic acid solution (also called as mixed solution of deionized water and acetic acid), and kneading.|[0046] In one embodiment, extrusion is preferably performed using a clover module.|[0047] In one embodiment, the temperature of drying is 110-130 ℃ and the time of drying is 1-4 hours.|[0048] In one embodiment, the firing temperature is 550-650 ℃ and the firing time is 2-4 hours.|[0049] The invention also provides a chromium modified alumina carrier, which is obtained by the preparation method, and the BET specific surface area of the chromium modified alumina carrier is 190-250m 2/g, and the pore volume is 0.65-0.75mL/g. Here, the chromium auxiliary agent is added into the main catalyst (alumina) to improve the acid type, increase the acid position number and the catalyst dispersivity, enhance the capability of adsorbing and dissociating hydrogen, further improve the hydrogenation activity of the carbon residue removal catalyst, reduce the carbon deposition generation rate and prolong the service life of the catalyst.|[0050] The invention also provides application of the chromium-modified alumina carrier, and the chromium-modified alumina carrier prepared by the preparation method is applied to residual oil hydrodecarbonization catalysts.|[0051] In the present invention, all the preparation materials are commercially available products well known to those skilled in the art unless specified otherwise.|[0052] The present invention will be described in detail with reference to examples and experimental examples. These are merely examples and are not intended to limit the present invention in any way.|[0053] The invention adopts a waste propane dehydrogenation catalyst to detect, and uses an X-ray fluorescence meter (XRF) to measure the element content, wherein the oxide of chromium accounts for 18.71 percent calculated by Cr 2O3, and the balance is Al 2O3 and a small amount of auxiliary agent. According to the alkali digestion flame atomic absorption spectrophotometry (HJ 687-2014) for determining hexavalent chromium of solid waste, the hexavalent chromium content in the total chromium is determined to be 31.20%.|[0054] Example 1|Step 1, crushing the waste catalyst, screening by adopting an 80-mesh quasi-screen, taking a screened sample, adding 1.1mol/L of dilute sulfuric acid, wherein the solid-to-liquid ratio of the sample to the dilute sulfuric acid is 1:15 (g/mL), namely, adding 1000g of waste catalyst powder into the dilute sulfuric acid, stirring for 20min at 50 ℃, filtering, and washing to obtain acid leaching filtrate of chromium-containing aluminum sulfate and wet alumina filter residues. Chromium and aluminum in the filtrate were measured by inductively coupled plasma emission spectrometry (ICP-OES) and the leaching rate of chromium was calculated to be 98.95% and the leaching rate of aluminum was calculated to be 17.84%.|[0055] And 2, adding sodium sulfite into acid leaching filtrate containing chromium aluminum sulfate for reduction according to the hexavalent chromium ratio, wherein the theoretical addition amount is 53.74g, the excess amount is 1.1 times, the actual addition amount is 59.12g, and the reduction time is 25min.|[0056] And 3, adding solid aluminum sulfate into the solution reduced in the step 2, adjusting the concentration of Cr 2O3 and Al 2O3 in the solution to be 3.3g/L and 125g/L respectively, and adjusting the pH to be 3.0 by adding sulfuric acid and sodium hydroxide solution to obtain the acidic solution of the chromium-containing aluminum sulfate.|[0057] And 4, taking 800g of wet alumina filter residue (solid content is 63.20%), adding 1710g of 32% sodium hydroxide solution, treating for 5 hours at 120 ℃ to obtain an alkaline solution containing sodium metaaluminate, adding deionized water to adjust the concentration of Al 2O3 to 200g/L, and cooling to 50 ℃ for standby.|[0058] And 5, adding the prepared acidic solution containing the chromium aluminum sulfate and the alkaline solution containing the sodium metaaluminate into a neutralization kettle in parallel, wherein the neutralization temperature is 60℃, pH and is 8.0, the retention time of materials in the neutralization kettle is 3.0h, and filtering, washing, drying and crushing the materials to obtain a powder finished product, wherein the Cr 2O3 content is 1.0%, the 600 ℃ burned residue is 65.80%, the pore volume is 1.02mL/g, and the specific surface area is 292m 2/g.|[0059] Step 6, preparing a chromium modified alumina carrier, namely taking 608g of powder, adding 12g of forming auxiliary sesbania powder and 4g of citric acid, mixing for 5min, adding a mixed solution of 500g of deionized water and 18g of concentrated nitric acid, kneading for 30min, extruding by using a 1.67 x 1.50 four-leaf grass module, drying at 120 ℃ for 4h, and roasting at 650 ℃ for 3h in a tube furnace to obtain a finished chromium modified alumina carrier product, and recording as S1.|[0060] Example 2|Step 1, crushing the waste catalyst, sieving the crushed waste catalyst by a 100-mesh standard sieve, taking a sieved sample, adding 1.0mol/L dilute sulfuric acid, wherein the solid-to-liquid ratio of the sample to the dilute sulfuric acid is 1:16 (g/mL), namely, adding 1000g of waste catalyst powder into the dilute sulfuric acid, stirring for 25min at 45 ℃, filtering and washing to obtain acid leaching filtrate containing chromium aluminum sulfate and wet alumina filter residues. Chromium and aluminum in the filtrate were measured by ICP-OES, and the leaching rate of chromium was calculated to be 99.10% and the leaching rate of aluminum was calculated to be 18.41%.|[0061] And 2, adding sodium sulfite as a reducing agent into the acid leaching filtrate containing chromium aluminum sulfate for reduction according to the hexavalent chromium proportion, wherein the theoretical addition amount is 142.48g, the excess amount is 1.1 times, the actual feeding amount is 156.72g, and the reduction time is 20min.|[0062] And 3, adding solid aluminum sulfate into the solution reduced in the step 2, adjusting the concentration of Cr 2O3 and Al 2O3 in the solution to be 5.55g/L and 140g/L respectively, and adjusting the pH to be 3.5 by adding sulfuric acid and sodium hydroxide solution to obtain the acidic solution of the chromium-containing aluminum sulfate.|[0063] Step 4, 800g of wet alumina filter residue (solid content 60.90%) is taken, 1650g of 32% sodium hydroxide solution is added, and the mixture is treated for 4 hours at the temperature of 125 ℃ to obtain alkaline solution containing sodium metaaluminate, deionized water is added to adjust the concentration of Al 2O3 to 224g/L, and the mixture is cooled to 50 ℃ for standby.|[0064] And 5, adding the prepared acidic solution containing the chromium aluminum sulfate and the alkaline solution containing the sodium metaaluminate into a neutralization kettle in parallel, wherein the neutralization temperature is 65℃, pH and the retention time of the materials in the neutralization kettle is 4.0h, and filtering, washing, drying and crushing the materials to obtain a powder finished product, wherein the Cr 2O3 content is 1.5%, the 600 ℃ burned residue is 65.50%, the pore volume is 1.00mL/g, and the specific surface area is 285m 2/g.|[0065] Step 6, preparing a chromium modified alumina carrier, namely taking 611g of powder, adding 8g of forming auxiliary sesbania powder and 8g of citric acid, mixing for 5min, adding 480g of deionized water and 22g of mixed solution of concentrated nitric acid, kneading for 25min, extruding by using a 1.67 x 1.50 four-leaf grass module, drying at 120 ℃ for 3h, and roasting in a tubular furnace at 650 ℃ for 3h to obtain a finished chromium modified alumina carrier product, and recording as S2.|[0066] Example 3|Step 1, crushing the waste catalyst, sieving the crushed waste catalyst by a 120-mesh standard sieve, taking a sieved sample, adding 1.0mol/L dilute sulfuric acid, wherein the solid-to-liquid ratio of the sample to the dilute sulfuric acid is 1:15 (g/mL), namely, adding 1000g of waste catalyst powder into the dilute sulfuric acid, stirring for 20min at 40 ℃, filtering and washing to obtain acid leaching filtrate containing chromium aluminum sulfate and wet alumina filter residues. Chromium and aluminum in the filtrate were measured by ICP-OES, and the leaching rate of chromium was calculated to be 98.76% and the leaching rate of aluminum was calculated to be 16.90%.|[0067] And 2, adding sodium metabisulfite serving as a reducing agent into the acid leaching filtrate containing chromium aluminum sulfate for reduction according to the hexavalent chromium proportion, wherein the theoretical addition amount is 108.07g, the excess amount is 1.2 times, the actual feeding amount is 129.68g, and the reduction time is 20min.|[0068] And 3, adding solid aluminum sulfate into the solution reduced in the step 2, adjusting the concentration of Cr 2O3 and Al 2O3 in the solution to 7.95g/L and 150g/L respectively, and adjusting the pH to 3.5 by adding sulfuric acid and sodium hydroxide solution to obtain the acidic solution of chromium-containing aluminum sulfate.|[0069] Step 4, 800g of wet alumina filter residue (solid content is 61.00%) is taken, 1650g of 32% sodium hydroxide solution is added, and the solution is treated for 3.5h at 130 ℃ to obtain alkaline solution containing sodium metaaluminate, deionized water is added to adjust the concentration of Al 2O3 to 240g/L, and the solution is cooled to 50 ℃ for standby.|[0070] And 5, adding the prepared acidic solution containing the chromium aluminum sulfate and the alkaline solution containing the sodium metaaluminate into a neutralization kettle in parallel, wherein the neutralization temperature is 55℃, pH and the retention time of the materials in the neutralization kettle is 3.5 hours, and filtering, washing, drying and crushing the materials to obtain a powder finished product, wherein the Cr 2O3 content is 2.0%, the 600 ℃ burned residue is 65.72%, the pore volume is 0.98mL/g, and the specific surface area is 278m 2/g.|[0071] Step 6, preparing a chromium modified alumina carrier, namely taking 609g of powder, adding 8g of guar gum powder as a forming additive and 8g of citric acid, mixing for 5min, adding 470g of mixed solution of deionized water and 14g of acetic acid, kneading for 35min, extruding by using a 1.67 x 1.50 four-leaf grass module, drying at 120 ℃ for 2h, and roasting in a tube furnace at 650 ℃ for 2h to obtain a finished chromium modified alumina carrier product, and recording as S3.|[0072] Example 4|Step 1, crushing the waste catalyst, sieving the crushed waste catalyst by a 100-mesh standard sieve, taking a sieved sample, adding 1.3mol/L of dilute sulfuric acid, wherein the solid-to-liquid ratio of the sample to the dilute sulfuric acid is 1:12.5 (g/mL), namely, adding 1000g of waste catalyst powder into the dilute sulfuric acid, stirring for 15min at 40 ℃, filtering and washing to obtain acid leaching filtrate containing chromium aluminum sulfate and wet aluminum oxide filter residues. Chromium and aluminum in the filtrate were measured by ICP-OES, and the leaching rate of chromium was calculated to be 99.05% and the leaching rate of aluminum was calculated to be 18.70%.|[0073] And 2, adding sodium bisulphite serving as a reducing agent into acid leaching filtrate containing chromium aluminum sulfate for reduction according to the ratio of hexavalent chromium, wherein the theoretical addition amount is 118.67g, the excess amount is 1.1 times, the actual feeding amount is 130.54g, and the reduction time is 25min.|[0074] And 3, adding solid aluminum sulfate into the solution reduced in the step 2, adjusting the concentration of Cr 2O3 and Al 2O3 in the solution to be 10.0g/L and 150g/L respectively, and adjusting the pH value to be 3.2 by adding sulfuric acid and sodium hydroxide solution to obtain the acidic solution of the chromium-containing aluminum sulfate.|[0075] And 4, taking 800g of wet alumina filter residue (with the solid content of 62.10%), adding 1680g of 32% sodium hydroxide solution, treating for 4 hours at the temperature of 120 ℃ to obtain an alkaline solution containing sodium metaaluminate, adding deionized water to adjust the concentration of Al 2O3 to 240g/L, and cooling to 50 ℃ for standby.|[0076] And 5, adding the prepared acidic solution containing the chromium aluminum sulfate and the alkaline solution containing the sodium metaaluminate into a neutralization kettle in parallel, wherein the neutralization temperature is 60℃, pH and the retention time of the materials in the neutralization kettle is 4.0h, and obtaining a powder finished product after filtering, washing, drying and crushing, wherein the Cr 2O3 content is 2.5%, the burned residue is 65.25% at 600 ℃, the pore volume is 0.97mL/g, and the specific surface area is 273m 2/g.|[0077] Step 6, preparing a chromium modified alumina carrier, namely taking 613g of powder, adding 8g of guar gum powder as a forming additive, 4g of hydroxypropyl cellulose and 8g of citric acid, mixing for 10min, adding a mixed solution of 465g of deionized water and 16g of acetic acid, kneading for 30min, extruding by using a 1.67 x 1.50 four-leaf grass module, drying at 120 ℃ for 2.5h, and roasting in a tube furnace at 650 ℃ for 3h to obtain a finished chromium modified alumina carrier product, and recording as S4.|[0078] Comparative example 1|The comparative example, in which solid aluminum sulfate was dissolved at a concentration of 150g/L each by directly using an aluminate sulfate solution as a raw material and the pH was adjusted to 3.5 by adding sulfuric acid and sodium hydroxide solution, was a chromium-free powder preparation process different from that of step 2 and step 3 of example 3. The remaining steps were the same as in example 3. The obtained powder has a residual baked at 600 ℃ of 66.20%, a pore volume of 1.04mL/g and a specific surface area of 290m 2/g.|[0079] The comparative example is that the preparation process of the chromium-free alumina carrier is different from that of the step 6 of the embodiment 3, 604g of powder is taken, 8g of guar gum powder as a forming additive and 8g of citric acid are added, the mixture is mixed for 5min, 470g of deionized water and 14g of acetic acid are added, the mixture is kneaded for 35min, 1.67 x 1.50 clover modules are used for extrusion, the drying is carried out for 2h at 120 ℃, and the roasting is carried out for 2h at 650 ℃ in a tube furnace, so that a chromium modified alumina carrier finished product is obtained and is marked as S5.|[0080] Comparative example 2|The comparative example was carried out using the chromium-free alumina carrier S5 prepared in comparative example 1 by an isovolumetric impregnation method with 2.0% Cr 2O3 supported thereon, and the obtained chromium-modified alumina carrier was designated as S6.|[0081] TABLE 1 index of chromium modified alumina supports|Table 1 shows the index of the chromium modified alumina carrier, and the BET specific surface area of the finished product of the chromium modified alumina carrier is 190-250m 2/g, and the pore volume is 0.65-0.75mL/g.|[0082] Application example 1 preparation of hydrogenation and carbon residue removal catalyst|The carriers prepared in examples 1, 2, 3 and 4 and comparative examples 1 and 2 are subjected to hydrogenation carbon residue removal catalyst preparation by adopting an isovolumetric impregnation method, specifically, high-purity molybdenum trioxide and basic nickel carbonate are dissolved by phosphoric acid to prepare impregnation liquid, the carriers are impregnated with active metals, and the corresponding catalysts are respectively marked as C1, C2, C3, C4, C5 and C6 after drying and roasting.|[0083] TABLE 2 index of residuum hydrodecarbonization catalyst|As shown in Table 2, the hydrodecarbonization catalysts C1, C2, C3 and C4 prepared by the invention and the hydrodecarbonization catalysts C5 and C6 prepared by the comparative example were respectively filled into a fixed bed hydrogenation reactor, and the catalytic performance of the catalysts was evaluated by taking atmospheric residuum as a raw material (the sulfur content in the raw material oil was 2.74wt%, the nitrogen content was 0.2815wt% and the trace carbon residue content was 10.97 wt%). The carbon residue value of the oil before and after the reaction is measured by adopting a micro carbon residue method, the carbon deposit content on the catalyst after the reaction is measured by adopting an infrared absorption method, and the relative carbon residue removal rate and the relative carbon deposit rate are calculated by taking the catalyst C5 prepared by the comparative example as a reference.|[0084] The reaction conditions are that the reaction temperature is 380 ℃, the pressure is 16.0MPa, the liquid hourly space velocity is 0.67h < -1 >, the hydrogen oil volume ratio is 700, the content of carbon residue in the generated oil is measured after the reaction is carried out for 720h, the carbon residue removal rate is calculated, and the evaluation result is shown in Table 3.|[0085] TABLE 3 evaluation of residuum hydrodecarbonization catalyst results|As shown in Table 3, after modification by adding chromium, the carbon removal rate of the catalyst was increased and the carbon deposition rate was decreased, and the carbon removal rate of the catalyst prepared by the method of the present invention was higher and the carbon deposition was less than that of examples C1 to C4 and comparative example C6.|[0086] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. (CN120479411)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the field of catalyst preparation, in particular to a chromium modified alumina carrier, a preparation method and application thereof.|BACKGROUND ART|[0002] In petroleum refining, oil which remains after vacuum distillation and corresponds to an atmospheric pressure of >500 ℃ is generally called Vacuum Residue (VR), and oil which remains after atmospheric distillation and corresponds to an atmospheric pressure of >350 ℃ is also called Atmospheric Residue (AR). The residual oil has complex composition, large average relative molecular mass, high viscosity, high carbon residue value, and large amount of harmful elements such as metal, sulfur, nitrogen, colloid, asphaltene and the like, and has high hydrotreating difficulty.|[0003] The fixed bed hydrogenation technology is the most mature and fast-growing processing means with the largest devices in the residuum hydrotreating process. The fixed bed hydrogenation adopts a catalyst grading technology, and is respectively filled with a plurality of protective agents (HG), demetallizing agents (HDM), desulfurizing agents (HDS) and carbon residue removing catalysts (HDCCR) according to a proper proportion, and hydrogenation reaction is carried out within a certain temperature range, so that hydrogenation products with qualified impurity contents such as metal, sulfur, nitrogen, carbon residue and the like are obtained.|[0004] With the increasing degradation of the processed raw materials, the carbon residue value of the raw materials is higher and higher, and the load of the carbon residue removal catalyst responsible for the deep conversion of carbon residue is higher and higher. Because the carbon residue removal catalyst is positioned at the tail end of the residual oil hydrogenation catalyst system, compared with other catalysts, the reaction temperature is high, the hydrogen partial pressure is low, and after the hydrogenation of the front-end catalyst, the colloid structure of the oil asphaltene is destroyed, so that the carbon residue removal catalyst Yi Shengjiao has the carbon deposit amount of generally up to 20 percent. The catalyst pore canal for removing carbon residue is relatively smaller, generally only tens or tens of nanometers, the diffusion resistance of the macromolecule in the reaction residue to the catalyst pore canal is relatively larger, carbon deposit is deposited on the outer side of the catalyst more, the pore diameter is further reduced, the inner diffusion control effect is more obvious, the macromolecule is more difficult to enter the inside of the catalyst pore canal and is continuously coked at the edge of the catalyst, the utilization rate of active sites in the catalyst pore canal is continuously reduced, and the catalyst deactivation is accelerated. Therefore, in order to improve the activity stability of the catalyst, researchers have focused on enhancing the anti-carbon deposition performance of the catalyst, improving the distribution of carbon deposition in the radial direction of the catalyst and improving the high temperature stability of the active phase.|[0005] At present, the following strategies are mainly adopted, namely, firstly, the acid strength, the acid quantity and the acid property of a carrier are regulated and controlled, and the generation rate of carbon deposition precursors is reduced, such as K, mg, B, F and the like are added. For example, chinese patent publication No. CN106622264a discloses a hydrodecarbonization catalyst, a preparation method and application thereof, the catalyst comprises an active metal component and a modified hydrogenation catalyst carrier, the modified hydrogenation catalyst carrier comprises a carrier, and a metal auxiliary and an acid auxiliary supported on the carrier, the metal auxiliary and the acid auxiliary are layered on the carrier, the shell layer is the metal auxiliary, the core layer is the acid auxiliary, the metal auxiliary is a group IA metal component and/or a group IIA metal component (e.g., mg, K, ca, etc.), and the acid auxiliary is at least one component selected from F, P and B. The hydrodecarbonization catalyst prepared by the method can obtain higher denitrification rate and carbon residue removal rate in the application of heavy oil hydrotreatment and has lower carbon deposit amount after heavy oil hydrotreatment, so the catalyst has high stability and long service life. Secondly, the number of diffusion holes is properly increased, the carbon deposition capacity is improved, the uniform distribution of carbon deposition in the radial direction of the catalyst is promoted, and the utilization rate of active sites in the holes is improved. For example, chinese patent publication No. CN103785397a discloses a hydrodecarbonization catalyst and a preparation method thereof. The alumina gel treated by high temperature and high pH aging has high crystallinity, less amorphous alumina and relatively larger crystal grains. The reduction of the amorphous alumina content promotes the increase of inter-particle voids, relatively uniform boehmite grain size and promotes the concentration of catalyst pore diameters. The catalyst prepared by uniformly mixing and shaping the alumina gel and the ammonium aluminum carbonate has concentrated pore distribution of 6-10nm and proper pore distribution of more than 100nm, and has low active component content and high carbon residue removal, metal removal and desulfurization activities. Third, the hydrogenation performance of the carrier active phase is improved. Chinese patent publication No. CN114643079a discloses a hydrogenation carbon residue removal catalyst, its preparation method and application. The hydrodecarbonization catalyst is used in the hydrodecarbonization process of heavy oil, can deeply remove polycyclic aromatic hydrocarbon and carbon residue in heavy oil, and has good stability. The molybdenum species form phosphomolybdenum blue micelle protected by the surfactant, so that the distribution of molybdenum in the catalyst is concentrated, and the molybdenum with higher polymerization degree is more favorable for forming high-stacking and long-platelet with improved upper-platelet clusters on the surface of the carrier after vulcanization, thereby obtaining the catalyst with lower intrinsic activation energy and more outstanding low-temperature activity. Meanwhile, as +5 molybdenum in the phosphomolybdenum blue is more easily vulcanized into +4 molybdenum disulfide, the molybdenum formation rate of molybdenum disulfide is increased, and the introduction of the complexing auxiliary agent delays the vulcanization of nickel, so that an active phase structure which takes MoS 2 as a framework and is formed in the catalyst and is formed by high-efficiency hydrogenation and dearomatization of metallic nickel on the outer surface is more easily realized.|[0006] Although the method can improve the performance and prolong the service life of the residual oil hydrodecarbonization catalyst, the method also has the problem of high production cost. The carbon residue removing agent is the variety with the highest active metal content in the residual oil hydrogenation series catalyst, and the price is the highest, so the catalyst is particularly sensitive to cost control. For the carbon residue removal catalyst, the cost of the active metal and the auxiliary agent accounts for about 70-80%, and the cost of the carrier accounts for about 20-30%. In recent years, a route for recovering active metals and alumina and preparing the catalyst by using waste catalysts as raw materials is paid attention to gradually, but the prior recovery technology still has the defects of low metal recovery rate, complex process flow, secondary pollution and the like. For example, chinese patent publication No. CN114602484a discloses a method for preparing a hydrodecarbonization catalyst, in which after the powder of the spent catalyst is decarbonized, ammonium bicarbonate is subjected to hydrothermal activation treatment, on the one hand, active metal molybdenum in the spent catalyst and vanadium deposited in the reaction process undergo dissolution reaction, and on the other hand, alumina in the spent catalyst undergoes hydrothermal crystallization reaction under airtight and weak alkaline hydrothermal conditions, and due to dissolution of metal molybdenum and vanadium and crystallization of alumina, the pore structure of the activated spent catalyst is well improved. The metakaolin is subjected to hydrothermal crystallization treatment by ammonium bicarbonate solution, the specific surface and pore volume are improved, etching points are formed on the surface of metakaolin grains, and the pore channel content of the material is improved by 10-20 nm. The above patents utilize waste catalysts, although achieving the effects of improving catalyst performance and reducing cost. However, the waste catalyst raw material is also stored in the charcoal burning process, the catalyst carbon deposit can be spontaneous-burned and generate open fire at 400-600 ℃, the high-temperature combustion is easy to cause the temperature of a material layer to fly, the temperature control is difficult, the charcoal is burned under the condition of the roasting temperature of 700-950 ℃, the molybdenum trioxide can be sublimated, and the molybdenum recovery rate is reduced.|[0007] Therefore, development of a method capable of preparing a catalyst with excellent performance for carbon residue removal and realizing efficient recycling of resources is needed.|DISCLOSURE|Disclosure of Invention|[0008] Aiming at the problems that the prior recovery technology still has low metal recovery rate, complex process flow, secondary pollution generation and the like, and the performance cannot meet the requirements, the invention provides a chromium modified alumina carrier and a preparation method and application thereof.|[0009] The technical method of the invention is as follows:| the preparation method of the chromium modified alumina carrier comprises the following steps: | S1, crushing, acid leaching and filtering a waste chromium propane dehydrogenation catalyst to obtain acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues, wherein chromium elements in the acid leaching filtrate containing chromium aluminum sulfate are III and VI; | S2, adding a reducing agent into the acid leaching filtrate containing the chromium aluminum sulfate, and reducing VI-valent chromium element in the acid leaching filtrate containing the chromium aluminum sulfate into III-valent chromium element to obtain a solution containing the chromium aluminum sulfate; | S3, adding aluminum sulfate into the acid leaching filtrate of the chromium-containing aluminum sulfate according to the chromium and aluminum content of the chromium-modified aluminum oxide carrier, and regulating the pH value by using sulfuric acid and a sodium hydroxide solution to obtain an acidic solution of the chromium-containing aluminum sulfate; | S4, alkali liquor is used for dissolving alumina filter residues to obtain an alkaline solution containing sodium metaaluminate; | s5, carrying out neutralization precipitation on an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate by adopting a neutralization method, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder; | S6, kneading, extruding, drying and roasting the chromium modified aluminum hydroxide powder and the forming auxiliary agent to obtain the chromium modified aluminum oxide carrier. |[0010] In the step S1, the product granularity of the crushed waste chromium propane dehydrogenation catalyst is 80-mesh standard sieve passing rate which is more than or equal to 98 percent. In the sulfuric acid leaching step, the concentration of the sulfuric acid solution is 0.5-1.5mol/L, the temperature of the acid leaching is 40-60 ℃, the time of the acid leaching is 10-30min, and the solid-liquid mass volume ratio of the crushed product of the waste chromium propane dehydrogenation catalyst to the sulfuric acid solution is 1 (10-20) g/mL. Here, the alumina filter residue is in an aqueous state, and may be optionally washed or not washed, and the alkali dissolution reaction is directly performed without washing by default for simplifying the process.|[0011] In the step S2, the reducing agent comprises one or more of sodium sulfite, sodium bisulfite and sodium metabisulfite, the mass ratio of the actual usage amount of the reducing agent to the theoretical value is (1.1-1.3): 1, and the reduction time is 20-40min.|[0012] In the step S3, aluminum sulfate is solid or liquid, sulfuric acid and sodium hydroxide solution are used for adjusting the pH value of acid leaching filtrate of chromium-containing aluminum sulfate to 3-4, and then the acid solution of chromium-containing aluminum sulfate is obtained, wherein the concentration of the acid solution is 100-200g/L calculated by Al 2O3.|[0013] In the step S4, the alkali liquor is sodium hydroxide solution, the mass concentration of the sodium hydroxide solution is 30% -35%, the mass ratio of the sodium hydroxide solution to the alumina filter residue dry base (without water) is 3.3-3.5, the temperature of the alkali dissolution reaction is 100-150 ℃, the time of the alkali dissolution reaction is 2-6h, and the concentration of the alkali solution containing sodium metaaluminate obtained after the alkali dissolution reaction is 150-300g/L calculated by Al 2O3.|[0014] In the step of S5, the step of the neutralization method comprises the steps of adding an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate into a neutralization kettle in parallel, controlling the pH value to be 7-10, reacting for 1-4 hours at 50-80 ℃ in the neutralization kettle, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder, wherein the content of Cr 2O3 is 0.5-3.0%.|[0015] In the step S6, the forming auxiliary agent comprises one or more of sesbania powder, citric acid, guar gum powder and hydroxypropyl cellulose, the roasting temperature is 550-650 ℃, and the roasting time is 2-4h.|[0016] The invention also provides a chromium modified alumina carrier, which is obtained by the preparation method, wherein the specific surface area of the chromium modified alumina carrier is 190-250m 2/g, and the pore volume is 0.65-0.75mL/g.|[0017] The invention also provides application of the chromium-modified alumina carrier, and the chromium-modified alumina carrier prepared by the preparation method is applied to residual oil hydrodecarbonization catalysts.|[0018] The beneficial effects of the invention are as follows:| 1. The invention provides a preparation method of a chromium modified alumina carrier based on a recovered waste chromium propane dehydrogenation catalyst, which is characterized in that chromium (Cr) and aluminum (Al) resources in a waste agent are efficiently separated and recovered, and a catalyst carrier with a pore structure is reconstructed through a neutralization reaction process. The catalyst carrier with the reconstructed pore structure can realize the uniform dispersion of chromium and obtain the specific surface area, the pore diameter and the pore volume which are suitable for the hydrogenation carbon residue removal catalyst. Specifically, the invention takes waste chromium propane dehydrogenation catalyst as raw materials, based on the main components of chromium oxide, aluminum oxide and chromium element which coexist in III valence and VI valence, firstly, sulfuric acid leaching is adopted to dissolve chromium to form acid leaching filtrate containing chromium aluminum sulfate, and alumina filter residues are produced at the same time, and aiming at the problem that VI valence chromium in the acid leaching filtrate is difficult to be directly precipitated in the subsequent neutralization reaction process, the VI valence chromium is converted into III valence chromium which is easy to precipitate by adding a reducing agent. Then, alkali dissolution reaction is carried out on the alumina filter residues, so that the alumina filter residues are converted into alkaline solution containing sodium metaaluminate. And finally, precisely controlling the pH value of the acid leaching filtrate and the contents of Cr and Al, neutralizing and precipitating the two solutions by a neutralization method, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder, adding a forming auxiliary agent, and then carrying out the processes of kneading, extruding, drying, roasting and the like to prepare the chromium modified aluminum oxide carrier. Through the process, the specific surface area of the carrier finished product reaches 190-250m < 2 >/g through a BET method, the pore volume is 0.65-0.75mL/g, the high-efficiency recovery of chromium and aluminum resources in the waste catalyst is realized, the catalyst prepared by the carrier has higher carbon residue removal rate and less carbon deposit, and the double targets of resource recovery and catalyst performance improvement are achieved. |[0019] 2. The invention realizes the full utilization of the waste chromium propane dehydrogenation catalyst, shortens the treatment process flow, reduces the production cost of the carrier, and simultaneously adopts a neutralization and uniform precipitation method to realize the uniform distribution of chromium element, thereby being beneficial to the improvement of the catalytic performance. The catalyst is applied to the residual oil hydrodecarbonization process, can improve the removal rate of residual oil carbon residue by the catalyst, reduce the carbon deposition generation rate and prolong the service life of the catalyst.|INVENTION MODE|Detailed Description|[0020] The following description of the present invention will be made clearly and fully, and it is apparent that the embodiments described are some, but not all, of the embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0021] The invention is characterized in that the residual oil hydrodecarbonization catalyst has the problems of high-temperature aggregation of active components, reduced activity, coverage of active centers and acid centers by carbon deposit and the like in use. The existing solutions can improve performance, but the production cost is high due to the high cost ratio of active metal and carrier. Based on the method, the active metal of the hydrogenation catalyst is recovered as a key break, the main current technology is a technology for recovering molybdenum, nickel and vanadium by alkali melting or a technology for recovering molybdenum, nickel and vanadium by acid dissolution, and a large amount of aluminum is dissolved out (about 10-20%) in the two technologies, so that the subsequent separation of molybdenum, nickel and vanadium is difficult, the technological process becomes complicated, and the residual carrier for recovering the active metal is difficult to recycle due to irreversible change of pore structure and surface acidity caused by deposited metal and carbon deposition. Meanwhile, the domestic propane dehydrogenation industry is vigorously developed, and a fixed bed Propane Dehydrogenation (PDH) process is favored because of the advantages of simple reactor structure and low investment cost. However, the chromium catalyst (Cr content is generally 5-20wt%, and the rest is alumina and a small amount of auxiliary agent) used by the catalyst is regenerated and used for many times, so that the activity is gradually reduced, and finally the recovery treatment is needed. Therefore, the invention can shorten the process flow, reduce the environmental pollution and recycle valuable metal resources (such as chromium) by recycling the waste chromium propane dehydrogenation catalyst, and avoid the dilemma of recycling the hydrogenation catalyst.|[0022] The invention provides a preparation method of a chromium modified alumina carrier, which comprises the following steps:| S1, crushing, acid leaching and filtering the waste chromium propane dehydrogenation catalyst to obtain acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues, wherein chromium elements in the acid leaching filtrate containing chromium aluminum sulfate are III and VI. |[0023] In one embodiment, comminution employs comminution equipment common in the art. The product granularity of the crushed waste chromium propane dehydrogenation catalyst is 80 mesh standard sieve passing rate more than or equal to 98 percent.|[0024] In one embodiment, the concentration of the sulfuric acid solution in the sulfuric acid leaching step is 0.5-1.5mol/L. For example, the concentration of the sulfuric acid solution may be 0.7mol/L, 1.2mol/L. The temperature of the acid leaching is 40-60 ℃. For example, the temperature may be 45 ℃, 50 ℃. The pickling time is 10-30min. For example, the time may be 15min, 20min. The solid-liquid mass volume ratio of the crushed product of the waste chromium propane dehydrogenation catalyst to the sulfuric acid solution is 1 (10-20) g/mL. For example, the solid-to-liquid ratio is 1:12g/mL, 1:15g/mL.|[0025] Specifically, the equation for sulfuric acid leaching is:|Al2O3+3H2SO4→Al2(SO4)3+3H2O|Cr2O3+3H2SO4→Cr2(SO4)3+3H2O|CrO3+H2O→H2CrO4|2H2CrO4→H2Cr2O7+3H2O| Cr 2O3 (III-valent chromium) is insoluble in water but soluble in sulfuric acid, cr 3+ ions are formed to enter pickle liquor, precipitation is easy to generate when meeting alkali, crO 3 (VI-valent chromium) is soluble in water but exists in a sulfuric acid system in a Cr 2O72-/CrO42- form, precipitation is not easy to generate when meeting alkali, and recovery is realized by reduction and conversion into III-valent chromium. |[0026] S2, adding a reducing agent into the acid leaching filtrate containing the chromium aluminum sulfate, and reducing VI-valent chromium element in the acid leaching filtrate containing the chromium aluminum sulfate into III-valent chromium element to obtain a solution containing the chromium aluminum sulfate.|[0027] In one embodiment, the reducing agent includes one or more of sodium sulfite (Na 2SO3), sodium bisulfite (NaHSO 3), sodium metabisulfite (Na 2S2O5).|[0028] Specifically, the equation for the reduction process is:|H2Cr2O7+3Na2SO3+3H2SO4→Cr2(SO4)3+3Na2SO4+4H2O|2H2Cr2O7+6NaHSO3+3H2SO4→2Cr2(SO4)3+3Na2SO4+8H2O|2H2Cr2O7+3Na2S2O5+3H2SO4→2Cr2(SO4)3+3Na2SO4+5H2O| in one embodiment, the mass ratio of the actual amount of the reducing agent to the theoretical value is (1.1-1.3): 1. The excessive reducing agent ensures that the VI-valent chromium is completely reduced. |[0029] In one embodiment, the reduction time is 20-40 minutes. For example, the temperature of the reduction may be 25min, 30min.|[0030] In the subsequent neutralization precipitation process, acid-base neutralization reaction is needed, and if VI-valent chromium exists, the VI-valent chromium cannot participate in the reaction to generate precipitation, so that the VI-valent chromium is converted into III-valent chromium which is easy to precipitate by adding a reducing agent to generate precipitation, and the VI-valent chromium is prevented from being wasted.|[0031] S3, adding aluminum sulfate into the acid leaching filtrate of the chromium-containing aluminum sulfate according to the chromium and aluminum content of the chromium-modified aluminum oxide carrier, and regulating the pH value by using sulfuric acid and a sodium hydroxide solution to obtain an acidic solution of the chromium-containing aluminum sulfate.|[0032] In one embodiment, the aluminum sulfate is a solid or a liquid, preferably a solid. According to the invention, aluminum sulfate is added according to the chromium and aluminum contents, and the chromium content of the generated aluminum hydroxide powder is regulated and controlled, so that the proportion of chromium in the alumina carrier is regulated, and finally the carbon residue removal performance is optimized.|[0033] In one embodiment, the pH is adjusted to 3-4 using sulfuric acid and sodium hydroxide solution to provide an acidic solution of chromium-containing aluminum sulfate at a concentration of 100-200g/L calculated as Al 2O3.|[0034] S4, alkali liquor is used for dissolving the alumina filter residues, and an alkaline solution containing sodium metaaluminate is obtained.|[0035] In one embodiment, the lye is sodium hydroxide solution. The concentration of the sodium hydroxide solution is 30% -35%. For example, the concentration may be 32%, 34%.|[0036] Specifically, the equation for the alkali dissolution reaction is:|Al2O3+2NaOH→2NaAlO2+H2O| in one embodiment, the mass ratio of sodium hydroxide solution to alumina filter residue dry basis (without water) is 3.3-3.5. For example, the mass ratio may be 3.4. |[0037] In one embodiment, the temperature of the alkali dissolution reaction is 100-150 ℃, the time of the hot alkali dissolution reaction is 2-6h, and the pressure of the alkali dissolution alumina filter residue reaction is normal pressure. For example, the temperature may be 120 ℃, 140 ℃. The time can be 3h or 4h.|[0038] In one embodiment, the alkali solution containing sodium metaaluminate obtained after the alkali dissolution reaction has a concentration of 150-300g/L calculated as Al 2O3.|[0039] S5, carrying out neutralization precipitation on the acidic solution containing chromium aluminum sulfate and the alkaline solution containing sodium metaaluminate by adopting a neutralization method, filtering, washing, drying and crushing to obtain the chromium modified aluminum hydroxide powder.|[0040] In one embodiment, the neutralization method comprises the steps of adding an acidic solution containing chromium aluminum sulfate and an alkaline solution containing sodium metaaluminate into a neutralization kettle in parallel, controlling the pH value to be 7-10, reacting for 1-4 hours at 50-80 ℃ in the neutralization kettle, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder, wherein the content of Cr 2O3 is 0.5-3.0%. Here, the number of times of washing with water may be 2 or more. Deionized water is used for water washing. The drying can be vacuum drying or natural drying. The comminution is carried out using comminution equipment which is customary in the art. The crushed granularity is 180 mesh standard sieve passing rate >98%.|[0041] In the invention, chromium element exists in an acidic solution containing chromium aluminum sulfate in the form of soluble ions (such as Cr 3+), the solution is acidic, an alkaline solution containing sodium metaaluminate is alkaline, the acidic solution and the alkaline solution are mixed and then undergo a neutralization reaction, and coprecipitation of aluminum hydroxide and chromium hydroxide is formed through acid-base neutralization, so that chromium components are dispersed more uniformly in a carrier precursor, the synergistic effect of a chromium auxiliary agent and an alumina carrier is promoted, and the performance of the chromium auxiliary agent is fully exerted.|[0042] The neutralization method provided by the invention is a short-flow and waste-free method.|[0043] S6, kneading, extruding, drying and roasting the chromium modified aluminum hydroxide powder and the forming auxiliary agent to obtain the chromium modified aluminum oxide carrier.|[0044] In one embodiment, the forming aid comprises one or more of sesbania powder, citric acid, guar gum powder, hydroxypropyl cellulose. Further, the forming aid may also include an acetic acid solution or a nitric acid solution.|[0045] In one embodiment, the kneading step comprises mixing chromium-modified aluminum oxide with one or more of sesbania powder, citric acid, guar gum powder and hydroxypropyl cellulose, and adding acetic acid solution (also called as mixed solution of deionized water and acetic acid), and kneading.|[0046] In one embodiment, extrusion is preferably performed using a clover module.|[0047] In one embodiment, the temperature of drying is 110-130 ℃ and the time of drying is 1-4 hours.|[0048] In one embodiment, the firing temperature is 550-650 ℃ and the firing time is 2-4 hours.|[0049] The invention also provides a chromium modified alumina carrier, which is obtained by the preparation method, and the BET specific surface area of the chromium modified alumina carrier is 190-250m 2/g, and the pore volume is 0.65-0.75mL/g. Here, the chromium auxiliary agent is added into the main catalyst (alumina) to improve the acid type, increase the acid position number and the catalyst dispersivity, enhance the capability of adsorbing and dissociating hydrogen, further improve the hydrogenation activity of the carbon residue removal catalyst, reduce the carbon deposition generation rate and prolong the service life of the catalyst.|[0050] The invention also provides application of the chromium-modified alumina carrier, and the chromium-modified alumina carrier prepared by the preparation method is applied to residual oil hydrodecarbonization catalysts.|[0051] In the present invention, all the preparation materials are commercially available products well known to those skilled in the art unless specified otherwise.|[0052] The present invention will be described in detail with reference to examples and experimental examples. These are merely examples and are not intended to limit the present invention in any way.|[0053] The invention adopts a waste propane dehydrogenation catalyst to detect, and uses an X-ray fluorescence meter (XRF) to measure the element content, wherein the oxide of chromium accounts for 18.71 percent calculated by Cr 2O3, and the balance is Al 2O3 and a small amount of auxiliary agent. According to the alkali digestion flame atomic absorption spectrophotometry (HJ 687-2014) for determining hexavalent chromium of solid waste, the hexavalent chromium content in the total chromium is determined to be 31.20%.|[0054] Example 1|Step 1, crushing the waste catalyst, screening by adopting an 80-mesh quasi-screen, taking a screened sample, adding 1.1mol/L of dilute sulfuric acid, wherein the solid-to-liquid ratio of the sample to the dilute sulfuric acid is 1:15 (g/mL), namely, adding 1000g of waste catalyst powder into the dilute sulfuric acid, stirring for 20min at 50 ℃, filtering, and washing to obtain acid leaching filtrate of chromium-containing aluminum sulfate and wet alumina filter residues. Chromium and aluminum in the filtrate were measured by inductively coupled plasma emission spectrometry (ICP-OES) and the leaching rate of chromium was calculated to be 98.95% and the leaching rate of aluminum was calculated to be 17.84%.|[0055] And 2, adding sodium sulfite into acid leaching filtrate containing chromium aluminum sulfate for reduction according to the hexavalent chromium ratio, wherein the theoretical addition amount is 53.74g, the excess amount is 1.1 times, the actual addition amount is 59.12g, and the reduction time is 25min.|[0056] And 3, adding solid aluminum sulfate into the solution reduced in the step 2, adjusting the concentration of Cr 2O3 and Al 2O3 in the solution to be 3.3g/L and 125g/L respectively, and adjusting the pH to be 3.0 by adding sulfuric acid and sodium hydroxide solution to obtain the acidic solution of the chromium-containing aluminum sulfate.|[0057] And 4, taking 800g of wet alumina filter residue (solid content is 63.20%), adding 1710g of 32% sodium hydroxide solution, treating for 5 hours at 120 ℃ to obtain an alkaline solution containing sodium metaaluminate, adding deionized water to adjust the concentration of Al 2O3 to 200g/L, and cooling to 50 ℃ for standby.|[0058] And 5, adding the prepared acidic solution containing the chromium aluminum sulfate and the alkaline solution containing the sodium metaaluminate into a neutralization kettle in parallel, wherein the neutralization temperature is 60℃, pH and is 8.0, the retention time of materials in the neutralization kettle is 3.0h, and filtering, washing, drying and crushing the materials to obtain a powder finished product, wherein the Cr 2O3 content is 1.0%, the 600 ℃ burned residue is 65.80%, the pore volume is 1.02mL/g, and the specific surface area is 292m 2/g.|[0059] Step 6, preparing a chromium modified alumina carrier, namely taking 608g of powder, adding 12g of forming auxiliary sesbania powder and 4g of citric acid, mixing for 5min, adding a mixed solution of 500g of deionized water and 18g of concentrated nitric acid, kneading for 30min, extruding by using a 1.67 x 1.50 four-leaf grass module, drying at 120 ℃ for 4h, and roasting at 650 ℃ for 3h in a tube furnace to obtain a finished chromium modified alumina carrier product, and recording as S1.|[0060] Example 2|Step 1, crushing the waste catalyst, sieving the crushed waste catalyst by a 100-mesh standard sieve, taking a sieved sample, adding 1.0mol/L dilute sulfuric acid, wherein the solid-to-liquid ratio of the sample to the dilute sulfuric acid is 1:16 (g/mL), namely, adding 1000g of waste catalyst powder into the dilute sulfuric acid, stirring for 25min at 45 ℃, filtering and washing to obtain acid leaching filtrate containing chromium aluminum sulfate and wet alumina filter residues. Chromium and aluminum in the filtrate were measured by ICP-OES, and the leaching rate of chromium was calculated to be 99.10% and the leaching rate of aluminum was calculated to be 18.41%.|[0061] And 2, adding sodium sulfite as a reducing agent into the acid leaching filtrate containing chromium aluminum sulfate for reduction according to the hexavalent chromium proportion, wherein the theoretical addition amount is 142.48g, the excess amount is 1.1 times, the actual feeding amount is 156.72g, and the reduction time is 20min.|[0062] And 3, adding solid aluminum sulfate into the solution reduced in the step 2, adjusting the concentration of Cr 2O3 and Al 2O3 in the solution to be 5.55g/L and 140g/L respectively, and adjusting the pH to be 3.5 by adding sulfuric acid and sodium hydroxide solution to obtain the acidic solution of the chromium-containing aluminum sulfate.|[0063] Step 4, 800g of wet alumina filter residue (solid content 60.90%) is taken, 1650g of 32% sodium hydroxide solution is added, and the mixture is treated for 4 hours at the temperature of 125 ℃ to obtain alkaline solution containing sodium metaaluminate, deionized water is added to adjust the concentration of Al 2O3 to 224g/L, and the mixture is cooled to 50 ℃ for standby.|[0064] And 5, adding the prepared acidic solution containing the chromium aluminum sulfate and the alkaline solution containing the sodium metaaluminate into a neutralization kettle in parallel, wherein the neutralization temperature is 65℃, pH and the retention time of the materials in the neutralization kettle is 4.0h, and filtering, washing, drying and crushing the materials to obtain a powder finished product, wherein the Cr 2O3 content is 1.5%, the 600 ℃ burned residue is 65.50%, the pore volume is 1.00mL/g, and the specific surface area is 285m 2/g.|[0065] Step 6, preparing a chromium modified alumina carrier, namely taking 611g of powder, adding 8g of forming auxiliary sesbania powder and 8g of citric acid, mixing for 5min, adding 480g of deionized water and 22g of mixed solution of concentrated nitric acid, kneading for 25min, extruding by using a 1.67 x 1.50 four-leaf grass module, drying at 120 ℃ for 3h, and roasting in a tubular furnace at 650 ℃ for 3h to obtain a finished chromium modified alumina carrier product, and recording as S2.|[0066] Example 3|Step 1, crushing the waste catalyst, sieving the crushed waste catalyst by a 120-mesh standard sieve, taking a sieved sample, adding 1.0mol/L dilute sulfuric acid, wherein the solid-to-liquid ratio of the sample to the dilute sulfuric acid is 1:15 (g/mL), namely, adding 1000g of waste catalyst powder into the dilute sulfuric acid, stirring for 20min at 40 ℃, filtering and washing to obtain acid leaching filtrate containing chromium aluminum sulfate and wet alumina filter residues. Chromium and aluminum in the filtrate were measured by ICP-OES, and the leaching rate of chromium was calculated to be 98.76% and the leaching rate of aluminum was calculated to be 16.90%.|[0067] And 2, adding sodium metabisulfite serving as a reducing agent into the acid leaching filtrate containing chromium aluminum sulfate for reduction according to the hexavalent chromium proportion, wherein the theoretical addition amount is 108.07g, the excess amount is 1.2 times, the actual feeding amount is 129.68g, and the reduction time is 20min.|[0068] And 3, adding solid aluminum sulfate into the solution reduced in the step 2, adjusting the concentration of Cr 2O3 and Al 2O3 in the solution to 7.95g/L and 150g/L respectively, and adjusting the pH to 3.5 by adding sulfuric acid and sodium hydroxide solution to obtain the acidic solution of chromium-containing aluminum sulfate.|[0069] Step 4, 800g of wet alumina filter residue (solid content is 61.00%) is taken, 1650g of 32% sodium hydroxide solution is added, and the solution is treated for 3.5h at 130 ℃ to obtain alkaline solution containing sodium metaaluminate, deionized water is added to adjust the concentration of Al 2O3 to 240g/L, and the solution is cooled to 50 ℃ for standby.|[0070] And 5, adding the prepared acidic solution containing the chromium aluminum sulfate and the alkaline solution containing the sodium metaaluminate into a neutralization kettle in parallel, wherein the neutralization temperature is 55℃, pH and the retention time of the materials in the neutralization kettle is 3.5 hours, and filtering, washing, drying and crushing the materials to obtain a powder finished product, wherein the Cr 2O3 content is 2.0%, the 600 ℃ burned residue is 65.72%, the pore volume is 0.98mL/g, and the specific surface area is 278m 2/g.|[0071] Step 6, preparing a chromium modified alumina carrier, namely taking 609g of powder, adding 8g of guar gum powder as a forming additive and 8g of citric acid, mixing for 5min, adding 470g of mixed solution of deionized water and 14g of acetic acid, kneading for 35min, extruding by using a 1.67 x 1.50 four-leaf grass module, drying at 120 ℃ for 2h, and roasting in a tube furnace at 650 ℃ for 2h to obtain a finished chromium modified alumina carrier product, and recording as S3.|[0072] Example 4|Step 1, crushing the waste catalyst, sieving the crushed waste catalyst by a 100-mesh standard sieve, taking a sieved sample, adding 1.3mol/L of dilute sulfuric acid, wherein the solid-to-liquid ratio of the sample to the dilute sulfuric acid is 1:12.5 (g/mL), namely, adding 1000g of waste catalyst powder into the dilute sulfuric acid, stirring for 15min at 40 ℃, filtering and washing to obtain acid leaching filtrate containing chromium aluminum sulfate and wet aluminum oxide filter residues. Chromium and aluminum in the filtrate were measured by ICP-OES, and the leaching rate of chromium was calculated to be 99.05% and the leaching rate of aluminum was calculated to be 18.70%.|[0073] And 2, adding sodium bisulphite serving as a reducing agent into acid leaching filtrate containing chromium aluminum sulfate for reduction according to the ratio of hexavalent chromium, wherein the theoretical addition amount is 118.67g, the excess amount is 1.1 times, the actual feeding amount is 130.54g, and the reduction time is 25min.|[0074] And 3, adding solid aluminum sulfate into the solution reduced in the step 2, adjusting the concentration of Cr 2O3 and Al 2O3 in the solution to be 10.0g/L and 150g/L respectively, and adjusting the pH value to be 3.2 by adding sulfuric acid and sodium hydroxide solution to obtain the acidic solution of the chromium-containing aluminum sulfate.|[0075] And 4, taking 800g of wet alumina filter residue (with the solid content of 62.10%), adding 1680g of 32% sodium hydroxide solution, treating for 4 hours at the temperature of 120 ℃ to obtain an alkaline solution containing sodium metaaluminate, adding deionized water to adjust the concentration of Al 2O3 to 240g/L, and cooling to 50 ℃ for standby.|[0076] And 5, adding the prepared acidic solution containing the chromium aluminum sulfate and the alkaline solution containing the sodium metaaluminate into a neutralization kettle in parallel, wherein the neutralization temperature is 60℃, pH and the retention time of the materials in the neutralization kettle is 4.0h, and obtaining a powder finished product after filtering, washing, drying and crushing, wherein the Cr 2O3 content is 2.5%, the burned residue is 65.25% at 600 ℃, the pore volume is 0.97mL/g, and the specific surface area is 273m 2/g.|[0077] Step 6, preparing a chromium modified alumina carrier, namely taking 613g of powder, adding 8g of guar gum powder as a forming additive, 4g of hydroxypropyl cellulose and 8g of citric acid, mixing for 10min, adding a mixed solution of 465g of deionized water and 16g of acetic acid, kneading for 30min, extruding by using a 1.67 x 1.50 four-leaf grass module, drying at 120 ℃ for 2.5h, and roasting in a tube furnace at 650 ℃ for 3h to obtain a finished chromium modified alumina carrier product, and recording as S4.|[0078] Comparative example 1|The comparative example, in which solid aluminum sulfate was dissolved at a concentration of 150g/L each by directly using an aluminate sulfate solution as a raw material and the pH was adjusted to 3.5 by adding sulfuric acid and sodium hydroxide solution, was a chromium-free powder preparation process different from that of step 2 and step 3 of example 3. The remaining steps were the same as in example 3. The obtained powder has a residual baked at 600 ℃ of 66.20%, a pore volume of 1.04mL/g and a specific surface area of 290m 2/g.|[0079] The comparative example is that the preparation process of the chromium-free alumina carrier is different from that of the step 6 of the embodiment 3, 604g of powder is taken, 8g of guar gum powder as a forming additive and 8g of citric acid are added, the mixture is mixed for 5min, 470g of deionized water and 14g of acetic acid are added, the mixture is kneaded for 35min, 1.67 x 1.50 clover modules are used for extrusion, the drying is carried out for 2h at 120 ℃, and the roasting is carried out for 2h at 650 ℃ in a tube furnace, so that a chromium modified alumina carrier finished product is obtained and is marked as S5.|[0080] Comparative example 2|The comparative example was carried out using the chromium-free alumina carrier S5 prepared in comparative example 1 by an isovolumetric impregnation method with 2.0% Cr 2O3 supported thereon, and the obtained chromium-modified alumina carrier was designated as S6.|[0081] TABLE 1 index of chromium modified alumina supports|Table 1 shows the index of the chromium modified alumina carrier, and the BET specific surface area of the finished product of the chromium modified alumina carrier is 190-250m 2/g, and the pore volume is 0.65-0.75mL/g.|[0082] Application example 1 preparation of hydrogenation and carbon residue removal catalyst|The carriers prepared in examples 1, 2, 3 and 4 and comparative examples 1 and 2 are subjected to hydrogenation carbon residue removal catalyst preparation by adopting an isovolumetric impregnation method, specifically, high-purity molybdenum trioxide and basic nickel carbonate are dissolved by phosphoric acid to prepare impregnation liquid, the carriers are impregnated with active metals, and the corresponding catalysts are respectively marked as C1, C2, C3, C4, C5 and C6 after drying and roasting.|[0083] TABLE 2 index of residuum hydrodecarbonization catalyst|As shown in Table 2, the hydrodecarbonization catalysts C1, C2, C3 and C4 prepared by the invention and the hydrodecarbonization catalysts C5 and C6 prepared by the comparative example were respectively filled into a fixed bed hydrogenation reactor, and the catalytic performance of the catalysts was evaluated by taking atmospheric residuum as a raw material (the sulfur content in the raw material oil was 2.74wt%, the nitrogen content was 0.2815wt% and the trace carbon residue content was 10.97 wt%). The carbon residue value of the oil before and after the reaction is measured by adopting a micro carbon residue method, the carbon deposit content on the catalyst after the reaction is measured by adopting an infrared absorption method, and the relative carbon residue removal rate and the relative carbon deposit rate are calculated by taking the catalyst C5 prepared by the comparative example as a reference.|[0084] The reaction conditions are that the reaction temperature is 380 ℃, the pressure is 16.0MPa, the liquid hourly space velocity is 0.67h < -1 >, the hydrogen oil volume ratio is 700, the content of carbon residue in the generated oil is measured after the reaction is carried out for 720h, the carbon residue removal rate is calculated, and the evaluation result is shown in Table 3.|[0085] TABLE 3 evaluation of residuum hydrodecarbonization catalyst results|As shown in Table 3, after modification by adding chromium, the carbon removal rate of the catalyst was increased and the carbon deposition rate was decreased, and the carbon removal rate of the catalyst prepared by the method of the present invention was higher and the carbon deposition was less than that of examples C1 to C4 and comparative example C6.|[0086] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. Family Number|(115651952)|115651952|Abstract|(CN120479411 A)|The invention provides a chromium - modified alumina carrier and a preparation method and application thereof . The preparation method of the chromium modified alumina carrier comprises the following steps : crushing a waste chromium propane dehydrogenation catalyst , carrying out acid leaching , and filtering to obtain an acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues ; adding a reducing agent into the filtrate , supplementing aluminum sulfate , and adjusting the pH value of the solution to obtain an acidic solution containing chromium aluminum sulfate ; carrying out alkali dissolution on the aluminum oxide filter residues by using alkali liquor to obtain an alkali solution containing sodium metaaluminate ; mixing the acidic solution and the alkaline solution , carrying out neutralization reaction , filtering , washing , drying and crushing to obtain chromium modified aluminum hydroxide powder ; and kneading , extruding , drying and roasting the powder and a forming aid to obtain the chromium - modified alumina carrier . According to the present invention , the waste - free complete utilization of the waste chromium propane dehydrogenation catalyst and the preparation of the chromium modified alumina carrier are achieved , and the prepared carrier can be used for preparing the residual oil hydrogenation carbon residue removal catalyst , such that the carbon residue removal rate can be easily improved , and the carbon deposition generation can be easily reduced . |CPC codes|(CN120479411 A)|B01J - 021/04 |B01J - 023/26 |B01J - 032/00 |B01J - 035/10/19 |B01J - 035/10/42 |B01J - 035/10/61 |IPC codes|(CN120479411 A)|B01J - 023/26 |B01J - 032/00 |B01J - 035/60 |B01J - 035/61 |B01J - 035/63 | Basic materials chemistry|Chemical engineering B01J-021/04|B01J-023/26|B01J-032/00|B01J-035/10/19|B01J-035/10/42|B01J-035/10/61|C10G-045/04|C10G-045/08|C10G-2300/1037|C10G-2300/202|C10G-2300/205|C10G-2300/70 B01J-021/04|B01J-023/26|B01J-032/00|B01J-035/10/19|B01J-035/10/42|B01J-035/10/61|C10G-045/04|C10G-045/08|C10G-2300/1037|C10G-2300/202|C10G-2300/205|C10G-2300/70 B01J-023/26|B01J-032/00|B01J-035/60|B01J-035/61|B01J-035/63|C10G-045/04 B01J-023/26|B01J-032/00|B01J-035/60|B01J-035/61|B01J-035/63|C10G-045/04 PENDING (CN120479411)|PENDING ALIVE (CN120479411)|ALIVE (CN120479411)|LEGAL DETAILS FOR CN120479411|Actual or expected expiration date=2045-05-28|Legal state=ALIVE|Status=PENDING|Event publication date=2025-05-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510700986|Application date=2025-05-28|Standardized application number=2025CN-0700986|Event publication date=2025-08-15|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120479411|Publication stage code=A|Publication date=2025-08-15|Standardized publication number=CN120479411|Event publication date=2025-08-15|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-09-02|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN120479411)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfrSIWi24qdT1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000078606022&ekey=2211&xpn=CN120479411&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=AT%252F9L5%252FKH7Qe%252BTu%252BOjZxC5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN120479411)|CN (CN120479411)|NAME=REZEL ENGINEERING CORP. , COUNTRY=CN (CN120479411)|NAME=ZHANG JUJIAN;CHENGDU HUAFENG PATENT OFFICE , REG=51223 (CN120479411)|CN (CN120479411)|NAME=ZHU WEI, COUNTRY=CN |NAME=YANG CHENGGONG|NAME=SHI ZONGBO|NAME=ZHUO RUNSHENG 0 1 Titre: (CN120479411)|Chromium-modified alumina carrier and preparation method and application thereof Résumé: (CN120479411)|The invention provides a chromium-modified alumina carrier and a preparation method and application thereof. The preparation method of the chromium modified alumina carrier comprises the following steps: crushing a waste chromium propane dehydrogenation catalyst, carrying out acid leaching, and filtering to obtain an acid leaching filtrate containing chromium aluminum sulfate and alumina filter residues; adding a reducing agent into the filtrate, supplementing aluminum sulfate, and adjusting the pH value of the solution to obtain an acidic solution containing chromium aluminum sulfate; carrying out alkali dissolution on the aluminum oxide filter residues by using alkali liquor to obtain an alkali solution containing sodium metaaluminate; mixing the acidic solution and the alkaline solution, carrying out neutralization reaction, filtering, washing, drying and crushing to obtain chromium modified aluminum hydroxide powder; and kneading, extruding, drying and roasting the powder and a forming aid to obtain the chromium-modified alumina carrier. According to the present invention, the waste-free complete utilization of the waste chromium propane dehydrogenation catalyst and the preparation of the chromium modified alumina carrier are achieved, and the prepared carrier can be used for preparing the residual oil hydrogenation carbon residue removal catalyst, such that the carbon residue removal rate can be easily improved, and the carbon deposition generation can be easily reduced. 93 Abstract gpt-4o-mini no The article focuses on a chromium-modified alumina carrier and its preparation method, which does not relate to accelerated weathering or CO₂ capture.
99 IN202641043067 IN202641043067 IN202641043067 118508361 IN202641043067 A 2026-04-10 [IN202641043067] 2026-04-03 2026-04-03 2026-04-10 (IN202641043067)|2046-04-03 (IN202641043067)|Mineral carbonation apparatus exploiting exothermic differential strain for continuous thermomechanical depassivation (IN202641043067)|The invention relates to a continuous mineral carbonation apparatus that solves the problem of reaction-limiting surface passivation without mechanical attrition. The apparatus comprises an insulated reactor vessel (110) containing a packed mineral bed (120) of crushed magnesium-silicate substrate particles (121). A fluid circulation system (130) flows a CO2-saturated acidic activation fluid (140) through the bed. The resulting exothermic carbonation precipitates a solid carbonate passivation layer (210) on an unreacted silicate core (220), generating localized exothermic reaction heat (230). A thermal mismatch controller (310) restricts fluid flow, ensuring the heat accumulates to exceed a predefined thermal fracture threshold of the shell. Differential thermal expansion induces severe differential thermal strain (240), causing spontaneous thermal fracture (250) of the layer. A continuous product separator (410) extracts the spalled carbonate fragments as a stable mineral slurry (420), providing continuous permanent carbon dioxide sequestration (430). Babu Bapatla Surendra|Priyanka Irukumalli (IN202641043067)|Babu Bapatla Surendra|Priyanka Irukumalli Babu Bapatla Surendra|Priyanka Irukumalli (IN202641043067)|Babu Bapatla Surendra|Priyanka Irukumalli (IN202641043067)|However, industrial-scale mineral carbonation is limited by surface passivation.| (IN202641043067)|1. A mineral carbonation apparatus for carbon dioxide sequestration, comprising an insulated reactor vessel (110) containing a packed mineral bed (120) of magnesium-silicate substrate particles (121), and a fluid circulation system (130) configured to flow a CO2-saturated, acidic activation fluid (140) through the packed mineral bed; characterised in that the apparatus further comprises: (a) a thermal mismatch controller (310) coupled to the fluid circulation system and a distributed temperature sensor array (311) distributed within the packed mineral bed; (b) wherein contact between the acidic activation fluid and the magnesium-silicate substrate particles initiates an exothermic carbonation reaction, precipitating a solid carbonate passivation layer (210) onto an unreacted silicate core (220) of the particles and generating localized exothermic reaction heat (230); (c) wherein the unreacted silicate core possesses a higher coefficient of thermal expansion than the precipitating solid carbonate passivation layer; and (d) wherein the thermal mismatch controller modulates a volumetric flow rate of the activation fluid to restrict convective heat loss, forcing the localized exothermic reaction heat to accumulate to a level sufficient to cause an induced differential thermal strain (240), mathematically defined by the equation ε = Δα · ΔT, to exceed a predefined thermal fracture threshold corresponding to a mechanical stress range of 2 MPa to 5 MPa, causing spontaneous thermal fracture (250) of the passivation layer.|5. A method of continuous mineral carbonation, comprising loading magnesium-silicate substrate particles (121) into an insulated reactor vessel (110) to form a packed mineral bed (120), and injecting a CO2-saturated, acidic activation fluid (140) through the bed via a fluid circulation system (130) to initiate an exothermic carbonation reaction that precipitates a solid carbonate passivation layer (210) onto an unreacted silicate core (220) of the particles; characterised by the steps of: (a) accumulating localized exothermic reaction heat (230) at the particle interface by restricting convective cooling via a thermal mismatch controller (310); (b) generating differential thermal strain (240) driven by a higher coefficient of thermal expansion of the unreacted silicate core relative to a lower-expansion of the solid carbonate passivation layer; (c) fracturing and spalling the solid carbonate passivation layer via spontaneous thermal fracture (250) when the differential thermal strain, calculated as ε = Δα · ΔT, is controlled such that it exceeds a predefined thermal fracture threshold corresponding to 2 MPa to 5 MPa of mechanical stress, exposing fresh reactive surface; and (d) extracting the spalled carbonate fragments via a continuous product separator (410) to yield a stable carbon sequestration product.|7. An integrated industrial carbon mineralization hardware architecture comprising a low-pressure, thermally insulated retention vessel containing a porous matrix of reactive silicate minerals, and a fluid injection circuit configured to percolate a pressurized, carbon-dioxide-rich aqueous solution through the porous matrix to initiate an exothermic precipitation of carbonates upon the mineral surfaces; characterised in that the architecture further comprises: (a) an automated thermodynamic control module configured to dynamically modulate the percolation flow rate based on internal temperature gradients; (b) wherein the automated thermodynamic control module restricts the flow rate to trap the exothermic heat of precipitation at a mineral-carbonate boundary layer; and (c) wherein trapping said exothermic heat forces a differential thermal strain, mathematically defined as ε = Δα · ΔT, to exceed a mechanical stress threshold of 2 MPa to 5 MPa between the reactive silicate minerals and the precipitated carbonates, physically shattering the precipitated carbonate layer.| (IN202641043067)|The invention defines a specific reactor architecture that deliberately accumulates exothermic reaction heat to exceed a defined fracture threshold to actuate a controlled mechanical depassivation mechanism.|The invention relates to a continuous mineral carbonation apparatus that solves the problem of reaction-limiting surface passivation without mechanical attrition.|The present invention relates generally to carbon dioxide sequestration, industrial chemical reactors, and geochemical processing. More specifically, the invention relates to a continuous mineral carbonation apparatus that exploits the exothermic heat of reaction to physically fracture a forming carbonate passivation layer.| (IN202641043067)|MINERAL CARBONATION(100,9)|THERMOMECHANICAL DEPASSIVATION(100,2)|EXOTHERMIC DIFFERENTIAL STRAIN(100,1)|PACKED MINERAL BED(69,13)|UNREACTED SILICATE CORE(60,8)|EXOTHERMIC CARBONATION REACTION(57,2)|SPONTANEOUS THERMAL FRACTURE(48,8)|MISMATCH CONTROLLER(46,12)|CARBONATE EXOTHERMIC PRECIPITATION(45,1)|ACIDIC ACTIVATION FLUID(44,3)|DIFFERENTIAL THERMAL STRAIN(41,6)|RESTRICTING CONVECTIVE COOLING(39,1)|INSULATED RETENTION VESSEL(36,1)|MAGNESIUM SILICATE SUBSTRATE PARTICLE(35,8)|SILICATE MINERAL REACTION(35,2)|EXOTHERMIC PRECIPITATION(35,1)|POROUS MATRIX(33,2)|SUBSTRATE PARTICLE(31,8)|CARBONATE PRECIPITATION(30,1)|PRECIPITATION EXOTHERMIC HEAT(30,1)|CARBON MINERALIZATION HARDWARE ARCHITECTURE(29,1)|REACTOR VESSEL INSULATION(27,11)|EXOTHERMIC HEAT(27,5)|UNREACTED SILICATE(26,2)|RETENTION VESSEL(24,1)|THERMOMECHANICAL DEPASSIVATION CYCLE(23,4)|INDUSTRIAL SCALE MINERAL CARBONATION(23,1)|PRECIPITATED CARBONATE LAYER(23,1)|LOCALIZED EXOTHERMIC REACTION HEAT(22,3)|MAGNESIUM SILICATE(21,9)|REACTOR ARCHITECTURE(21,2)|LOCALIZED EXOTHERMIC REACTION(21,1)|PRECIPITATING SOLID(21,1)|FRACTURE THRESHOLD(20,2)|INDUCED DIFFERENTIAL THERMAL STRAIN(20,2)|MICROSCOPIC FRAGMENT(20,1)|STABLE MINERAL SLURRY(19,5)|PARTICULATE SUSPENSION(19,3)|SOLID CARBONATE PASSIVATION LAYER(18,4)|AUTOMATED THERMODYNAMIC CONTROL MODULE(18,2)|GEOCHEMICAL PROCESSING(18,1)|IMMEDIATE SURGE(18,1)|STABLE CARBON SEQUESTRATION(18,1)|ATTRITION(17,2)|PARTICLE INTERFACE(16,2)|FRACTURING(16,1)|SHELL THRESHOLD(16,1)|EXOTHERMIC REACTION HEAT(15,9)|CARBON DIOXIDE SEQUESTRATION(15,3)|CONTROLLED MECHANICAL DEPASSIVATION(15,1)|FRAGMENT(15,1)|PASSIVATION LAYER(14,16)|CONTINUOUS PRODUCT SEPARATOR(13,7)|CONVECTIVE HEAT LOSS(13,1)|EFFLUENT FLUID PORT(13,1)|FLUID INJECTION CIRCUIT(13,1)|MECHANICAL STRESS THRESHOLD(13,1)|BED(12,3)|CALCULATED FRACTURE LIMIT(12,1)|INDUSTRIAL CHEMICAL REACTOR(12,1)|PASSIVATION LAYER FRACTURE(12,1)|PERMANENT CARBON DIOXIDE SEQUESTRATION(12,1)|MINERAL CARBONATE BOUNDARY LAYER(11,1)|MODULATE PERCOLATION FLOW RATE(11,1)|CARBONATE PASSIVATION LAYER(10,2)|SURFACE PASSIVATION(10,1)|ACCELERATION(9,1)|EXOTHERMIC REACTION(9,1)|FLUID CIRCULATION SYSTEM(8,12)|DIFFERENTIAL THERMAL EXPANSION(8,3)|INORGANIC SURFACE(8,1)|CARBON SEQUESTRATION(7,6)|BOUNDARY LAYER(7,1)|CARBONATION REACTION RATE(7,1)|CRUSHED UNCALCINED OLIVINE(7,1)|INTERNAL REACTOR TEMPERATURE(7,1)|CONTROLLER OUTPUT(6,2)|INTERNAL TEMPERATURE GRADIENT(6,2)|SURFACE REACTION(6,2)|ACTIVATION VOLUMETRIC FLOW RATE(6,1)|MECHANICAL STRESS RANGE(6,1)|REACTION LIMITING SURFACE PASSIVATION(6,1)|SEEKING PERMANENT MINERAL SEQUESTRATION(6,1)|DISTRIBUTED TEMPERATURE SENSOR ARRAY(5,5)|AMORPHOUS SILICA(5,3)|MECHANICAL STRESS(5,3)|CONTROL MODULE(5,2)|PASSIVATION SURFACE(5,2)|UNREACTED SILICATE SUBSTRATE(5,2)|CARBONATION ENTHALPY(5,1)|VERIFIABLE CARBON CREDITING(5,1)|TEMPERATURE SENSOR ARRAY(4,5)|CARBONATE SHELL(4,3)|FIXED CARBON SEQUESTRATION(4,3)|FLUID EFFLUENT PORT(4,3)|PASSIVATION SHELL(4,2)|SILICATE CORE(4,2)|CARBON MINERALIZATION ARCHITECTURE(4,1)|COARSELY CRUSHED MAGNESIUM SILICATE(4,1)|CONVECTIVE COOLING RESTRICTION(4,1)|EXOTHERMIC PASSIVATION(4,1)|FRACTURED MICROFLAKE(4,1)|GEOLOGICALLY STABLE CO2 SEQUESTRATION(4,1)|INSTANTANEOUS LOCALIZED THERMAL ANOMALY(4,1)|MINERAL CARBONATION REACTING CO2(4,1)|PROTON PROMOTED SILICATE DISSOLUTION(4,1)|SILICATE CARBONATION(4,1)|SUSTAINED CARBONATION(4,1)|SUSTAINING CARBON MINERALIZATION(4,1)|THERMOMECHANICAL PHYSICS(4,1)|ULTRAFINE MILLING(4,1)|UNREACTED SILICATE PARTICLE(4,1)|STRAIN(3,5)|VOLUMETRIC FLOW RATE(3,5)|THERMAL EXPANSION VECTOR(3,3)|CO2 DISSOLUTION(3,2)|MINERAL BED(3,2)|PUMP CONTROL(3,2)|ATMOSPHERIC LEAKAGE MINIMAL RISK(3,1)|CARBON DIOXIDE PERMANENT SEQUESTRATION(3,1)|COARSE MINERAL SUBSTRATE(3,1)|COMPUTATIONAL ARCHITECTURE(3,1)|CRITICAL PREDEFINED THERMAL(3,1)|CRUSHED SILICATE(3,1)|EXOTHERMIC DIFFERENTIAL EXPANSION PHYSICS(3,1)|FLOW RATE(3,1)|FRACTURE EVENT TRIGGER(3,1)|GLOBAL MITIGATION(3,1)|HARD NUMERIC THRESHOLD CRITERIA(3,1)|IMPERMEABLE BARRIER(3,1)|INSULATED REACTOR TANK(3,1)|INTERFACIAL SHEAR STRESS(3,1)|INTERSTITIAL VOID SPACE(3,1)|LOCALIZED HEAT ACCUMULATION(3,1)|MICROSCOPIC DUST(3,1)|MINERAL AGGREGATE(3,1)|MINERAL SLURRY(3,1)|PACKED REACTOR BED(3,1)|PASSIVATED CARBONATION RATE CURVE(3,1)|PASSIVATION LAYER THERMOMECHANICAL FAILURE(3,1)|PERMANENT CARBON MINERALIZATION(3,1)|PROCEDURAL LOGIC(3,1)|ROCK CORE(3,1)|ROCK PARTICLE(3,1)|SALINE WASTE FLUID(3,1)|SILICATE EXPOSURE(3,1)|SILICATE MINERAL CARBONATION(3,1)|SILICATE MINERAL PACKED BED(3,1)|STONE GRINDING(3,1)|STRUCTURAL MISMATCH(3,1)|SUSTAINED THERMOMECHANICAL RATE CURVE(3,1)|THERMOMECHANICAL CYCLE(3,1)|TITANIUM LINED AUTOCLAVE(3,1)|ULTRAFINE POWDER(3,1)|UNREACTED CORE(3,1)|VALORIZE INDUSTRIAL WASTEWATER(3,1)|VARIABLE FREQUENCY DRIVE PUMP(2,5)|SHELL THERMAL EXPANSION(2,2)|CALCIUM RICH SILICATE(2,1)|CO2 SATURATED ACTIVATION(2,1)|EMITTED CO2(2,1)|ENERGY INTENSIVE CRUSHER(2,1)|EXTRACTED MINERAL SOLID(2,1)|FLUID PERCOLATION(2,1)|INDUSTRIAL MINERAL WOOL(2,1)|K THERMOCOUPLE(2,1)|LOCALIZED HEAT GENERATION(2,1)|LOCALIZED TEMPERATURE SPIKE(2,1)|LOW PRESSURE(2,1)|MAGNESIUM RICH SILICATE MINERAL(2,1)|MITIGATION SOLUTION(2,1)|NORMALIZE INPUT NOISE(2,1)| (IN202641043067)|1. A mineral carbonation apparatus for carbon dioxide sequestration, comprising an insulated reactor vessel (110) containing a packed mineral bed (120) of magnesium-silicate substrate particles (121), and a fluid circulation system (130) configured to flow a CO2-saturated, acidic activation fluid (140) through the packed mineral bed; characterised in that the apparatus further comprises: (a) a thermal mismatch controller (310) coupled to the fluid circulation system and a distributed temperature sensor array (311) distributed within the packed mineral bed; (b) wherein contact between the acidic activation fluid and the magnesium-silicate substrate particles initiates an exothermic carbonation reaction, precipitating a solid carbonate passivation layer (210) onto an unreacted silicate core (220) of the particles and generating localized exothermic reaction heat (230); (c) wherein the unreacted silicate core possesses a higher coefficient of thermal expansion than the precipitating solid carbonate passivation layer; and (d) wherein the thermal mismatch controller modulates a volumetric flow rate of the activation fluid to restrict convective heat loss, forcing the localized exothermic reaction heat to accumulate to a level sufficient to cause an induced differential thermal strain (240), mathematically defined by the equation ε = Δα · ΔT, to exceed a predefined thermal fracture threshold corresponding to a mechanical stress range of 2 MPa to 5 MPa, causing spontaneous thermal fracture (250) of the passivation layer.|2. The mineral carbonation apparatus as claimed in claim 1, wherein the thermal mismatch controller (310) regulates the volumetric flow rate to maintain a continuous thermomechanical depassivation cycle (320); wherein the spontaneous thermal fracture (250) of the passivation layer (210) exposes the unreacted silicate core (220), initiating an acceleration in the carbonation reaction rate and generating an immediate surge in localized exothermic reaction heat (230).|3. The mineral carbonation apparatus as claimed in claim 1, wherein the apparatus further comprises a continuous product separator (410) hydraulically coupled to a fluid effluent port (132) of the insulated reactor vessel (110); wherein the flow of the activation fluid (140) mechanically sweeps microscopic fragments of the fractured passivation layer (210) out of the packed mineral bed (120) as suspended particulate; and wherein the continuous product separator extracts the suspended particulate to yield a stable mineral slurry (420) comprising solid carbonate and amorphous silica.|4. The mineral carbonation apparatus as claimed in claim 1, wherein the packed mineral bed (120) comprises magnesium-silicate substrate particles (121) crushed to a diameter strictly bounded between 50 µm and 500 µm.|5. A method of continuous mineral carbonation, comprising loading magnesium-silicate substrate particles (121) into an insulated reactor vessel (110) to form a packed mineral bed (120), and injecting a CO2-saturated, acidic activation fluid (140) through the bed via a fluid circulation system (130) to initiate an exothermic carbonation reaction that precipitates a solid carbonate passivation layer (210) onto an unreacted silicate core (220) of the particles; characterised by the steps of: (a) accumulating localized exothermic reaction heat (230) at the particle interface by restricting convective cooling via a thermal mismatch controller (310); (b) generating differential thermal strain (240) driven by a higher coefficient of thermal expansion of the unreacted silicate core relative to a lower-expansion of the solid carbonate passivation layer; (c) fracturing and spalling the solid carbonate passivation layer via spontaneous thermal fracture (250) when the differential thermal strain, calculated as ε = Δα · ΔT, is controlled such that it exceeds a predefined thermal fracture threshold corresponding to 2 MPa to 5 MPa of mechanical stress, exposing fresh reactive surface; and (d) extracting the spalled carbonate fragments via a continuous product separator (410) to yield a stable carbon sequestration product.|6. The method as claimed in claim 5, wherein if a control logic circuit (312) within the thermal mismatch controller (310) detects that an internal reactor temperature is falling below a calculated fracture limit, the controller outputs a pump control signal (314) to a variable frequency drive pump (135) to reduce a volumetric flow rate of the fluid circulation system (130) to minimize convective heat extraction from the packed mineral bed (120).|7. An integrated industrial carbon mineralization hardware architecture comprising a low-pressure, thermally insulated retention vessel containing a porous matrix of reactive silicate minerals, and a fluid injection circuit configured to percolate a pressurized, carbon-dioxide-rich aqueous solution through the porous matrix to initiate an exothermic precipitation of carbonates upon the mineral surfaces; characterised in that the architecture further comprises: (a) an automated thermodynamic control module configured to dynamically modulate the percolation flow rate based on internal temperature gradients; (b) wherein the automated thermodynamic control module restricts the flow rate to trap the exothermic heat of precipitation at a mineral-carbonate boundary layer; and (c) wherein trapping said exothermic heat forces a differential thermal strain, mathematically defined as ε = Δα · ΔT, to exceed a mechanical stress threshold of 2 MPa to 5 MPa between the reactive silicate minerals and the precipitated carbonates, physically shattering the precipitated carbonate layer. (IN202641043067)|Field of the Invention|[0001] The present invention relates generally to carbon dioxide sequestration, industrial chemical reactors, and geochemical processing. More specifically, the invention relates to a continuous mineral carbonation apparatus that exploits the exothermic heat of reaction to physically fracture a forming carbonate passivation layer. By thermally isolating a packed bed of silicate minerals and circulating an acidic, CO2-bearing fluid, the apparatus induces a localized temperature rise at the reaction front. By utilizing the differential coefficient of thermal expansion between the unreacted silicate substrate and the forming carbonate product layer, the system generates sufficient mechanical strain to continuously spall the barrier, sustaining carbon mineralization without requiring high-pressure autoclaves or external mechanical agitation. The invention defines a specific reactor architecture that deliberately accumulates exothermic reaction heat to exceed a defined fracture threshold to actuate a controlled mechanical depassivation mechanism.|Background of the Invention|[0002] Global mitigation of anthropogenic climate change involves the permanent sequestration of carbon dioxide (CO2). Mineral carbonation-reacting CO2 with magnesium- or calcium-rich silicate rocks to form stable solid carbonates-is a method of permanent carbon storage possessing minimal risk of atmospheric leakage. However, industrial-scale mineral carbonation is limited by surface passivation. As the carbonation reaction proceeds, the resulting solid carbonate and amorphous silica precipitate directly onto the surface of the unreacted silicate particle. This product layer forms an impermeable barrier that blocks further CO2 and water from accessing the unreacted core, causing the reaction rate to drop and stalling the process.|[0003] Mitigation solutions in the prior art rely on external continuous depassivation methods. These include grinding the rock to ultra-fine powders (< 10 µm) which incurs substantial additional energy requirements, processing the slurry in titanium-lined autoclaves at elevated temperatures and pressures (e.g., 150°C and 150 atm), or utilizing continuous mechanical attrition milling. Concurrently, industrial operations generate significant volumes of hot, acidic, highly saline waste fluid containing dissolved CO2. Operators allocate substantial resources treating and reinjecting this fluid.|[0004] An apparatus is required that addresses surface passivation without requiring continuous external mechanical or chemical energy inputs. The carbonation of silicate minerals such as Olivine is highly exothermic (ΔH = -89 kJ/mol). If a reactor isolates this heat at the particle interface, the localized temperature spike exploits the differing thermal expansion coefficients between the silicate core and the carbonate shell. The accumulated heat generates mechanical stress to continuously fracture and spall the passivation layer, yielding a continuous low-pressure reactor capable of permanent carbon mineralization.|Technical Problem and Solution|[0005] Core Technical Problem: Industrial processes react carbon dioxide with crushed silicate rock to transform the gas into solid mineral states. As the gas converts into a solid carbonate on the surface of the rock particle, it creates a passivation shell. This shell blocks the remaining gas from reaching the interior of the rock, halting the reaction. To break this shell, prior art industrial plants use energy-intensive crushers to grind the rock into microscopic dust or use high-pressure vessels to force the gas through the shell. These external methods consume substantial electrical energy.|[0006] Proposed Technical Solution: The present invention minimizes the reliance on external crushers or high-pressure vessels by utilizing an engineered reactor design that forces the rock to fracture its own passivation shell. The reaction between CO2 and the silicate rock releases a significant amount of heat. The invention utilizes an insulated reactor tank to trap this heat where the shell is forming, while actively controlling the flow of fluid to ensure the heat builds up to a predefined breaking point. The newly formed carbonate shell and the original rock core expand at different rates when heated. The trapped heat causes the core to expand faster than the shell, creating internal stress that shatters and flakes off the shell. This exposes fresh rock, which reacts with more gas, generating more heat to shatter the next layer in a continuous thermomechanical cycle.|Objects of the Invention|[0007] The primary object of the invention is to provide a mineral carbonation apparatus that executes continuous carbon sequestration without requiring external mechanical attrition or high-pressure autoclaves.|[0008] Another object is to physically exploit the exothermic heat of reaction as a mechanical fracture mechanism. By thermally isolating a packed reactor bed, the apparatus harnesses the enthalpy of carbonation to generate a localized ΔT of 15°C to 50°C at the solid-liquid reaction front.|[0009] A further object is to utilize differential thermal expansion for continuous, controlled depassivation. The apparatus relies on the structural mismatch between the Coefficient of Thermal Expansion (CTE) of the unreacted silicate substrate (α ≈ 12.4 x 10^-6 K^-1) and the precipitating carbonate passivation layer (α ≈ 9.5 x 10^-6 K^-1). The resulting thermal strain is accumulated to intentionally exceed the tensile strength of the carbonate layer, where the predefined thermal fracture threshold corresponds to a stress range of approximately 2 to 5 MPa, forcing the layer to crack and spall.|[0010] A still further object is to establish a thermomechanical depassivation cycle. As the passivation layer spalls, fresh silicate surface is exposed, increasing the carbonation rate. This increased rate generates additional exothermic heat, driving further thermal mismatch and spalling.|[0011] A final object is to valorize industrial wastewater. The apparatus comprises a fluid circulation system configured to accept hot, acidic, CO2-laden water from industrial operations. The low pH accelerates proton-promoted silicate dissolution, while the elevated fluid temperature lowers the required activation energy.|Summary of the Invention|[0012] The present invention discloses a carbon mineralization architecture that harnesses the thermodynamic waste heat of silicate carbonation to continuously destroy its reaction-limiting passivation barrier through a closed-loop flow control system.|[0013] The apparatus comprises an Insulated Reactor Vessel housing a Packed Mineral Bed consisting of coarsely crushed magnesium-silicate rock with a particle size ranging from 50 to 500 µm. A Fluid Circulation System continuously flows an acidic, CO2-saturated Activation Fluid through the packed bed.|[0014] As the CO2 reacts with the silicate, a Passivation Layer of solid carbonate and silica precipitates onto the particles. Simultaneously, the Exothermic Reaction Heat elevates the temperature at the particle-fluid interface. Due to the Differential Thermal Expansion between the silicate core and the carbonate shell, significant interfacial shear stress is generated. A Thermal Mismatch Controller modulates the fluid flow to ensure the localized heat accumulation intentionally exceeds a predefined Thermal Fracture Threshold of the passivation layer. This flow modulation is utilized specifically to induce thermomechanical failure of the passivation layer.|[0015] The layer undergoes Spontaneous Thermal Fracture and spalls off into the fluid stream as suspended particulate, continuously exposing fresh reactive surface. The fluid stream carries the solid carbonate products out of the reactor to a separation unit, yielding geologically stable CO2 sequestration alongside mineral aggregate.|Brief Description of the Accompanying Drawings|[0016] FIG. 1 is a structural and thermodynamic schematic illustrating the insulated reactor vessel, the packed mineral bed, and the fluid circulation system, including the outputs for the stable mineral slurry and permanent carbon sequestration.|[0017] FIG. 2 illustrates the Exothermic Differential-Expansion Physics, detailing the formation of the passivation layer, the localized heat generation, and the resulting thermal strain that causes engineered spalling.|[0018] FIG. 3 provides a graphical representation of the Reaction Rate Kinetics along defined axes, contrasting the decline of a passivated system against the sustained carbonation rate of the present apparatus.|[0019] FIG. 4 depicts the Thermomechanical Depassivation Control Logic, showing how the Thermal Mismatch Controller modulates fluid flow to maintain the critical fracture temperature.|Detailed Description of the Invention|A. Hardware Architecture and Mineral Processing|[0020] The core system comprises an Insulated Reactor Vessel (110) constructed of industrial alloys or composite liners, rated for continuous low-pressure operation in the range of 1 to 10 atm. The vessel houses a Packed Mineral Bed (120) comprising magnesium-rich silicate minerals in the form of Magnesium-Silicate Substrate Particles (121). The minerals are comminuted to a coarse particle size bounded strictly between 50 µm and 500 µm, establishing sufficient interstitial void space for fluid percolation.|[0021] A Fluid Circulation System (130) drives an Activation Fluid (140) through the bed. The Fluid Circulation System (130) routes fluid into the vessel via a Fluid Injection Port (131) and extracts it via a Fluid Effluent Port (132). The fluid is heavily doped with CO2 to achieve an acidic state bounded between pH 3.5 and 6.0. The Activation Fluid comprises aqueous streams heated to temperatures between 60°C and 100°C.|B. Exothermic Passivation and Differential Expansion|[0022] As detailed in FIG. 2, the dissolved CO2 triggers dissolution of the silicate, precipitating a Passivation Layer (210) comprising solid carbonate and amorphous silica directly onto an Unreacted Silicate Core (220). The carbonation of the silicate material releases Exothermic Reaction Heat (230) quantified by an enthalpy of ΔH = -89 kJ/mol. Because the Insulated Reactor Vessel (110) restricts thermal dissipation, this heat creates a localized ΔT of 15°C to 50°C directly at the reaction front.|[0023] The Unreacted Silicate Core possesses a Coefficient of Thermal Expansion (CTE) of α ≈ 12.4 x 10^-6 K^-1, while the Passivation Layer possesses a lower CTE of α ≈ 9.5 x 10^-6 K^-1. The Core Thermal Expansion Vectors (221) drastically exceed the Shell Thermal Expansion Vectors (211), creating interfacial shear. The localized ΔT induces severe Differential Thermal Strain (240) determined mathematically by the equation ε = Δα · ΔT.|[0024] The resulting thermal stress (σ = E · ε) is forced to accumulate to a level sufficient to cause the induced differential thermal strain to intentionally exceed a predefined thermal fracture threshold corresponding to a mathematically calculated mechanical stress range of 2 MPa to 5 MPa. This engineered internal shear stress forces the layer to undergo Spontaneous Thermal Fracture (250), spalling the barrier away from the core.|C. Thermodynamic Control and Cycle Maintenance|[0025] The apparatus utilizes a Thermal Mismatch Controller (310) which continuously monitors the internal temperature gradient via a Distributed Temperature Sensor Array (311). As graphed in FIG. 4, the Distributed Temperature Sensor Array (311) transmits data via a Feedback Signal Pathway (313) to a Control Logic Circuit (312). If the temperature at the reaction front drops, the thermal strain becomes insufficient to fracture the passivation layer. The controller outputs a Pump Control Signal (314) to a Variable Frequency Drive Pump (135) to reduce the volumetric flow rate of the Activation Fluid (140). This reduces convective heat loss (Qloss), forcing the Exothermic Reaction Heat (230) to accumulate locally until it breaches the critical predefined thermal fracture threshold.|[0026] Once fracture occurs, the exposure of fresh silicate triggers a spike in carbonation, generating new heat. This establishes a continuous Thermomechanical Depassivation Cycle (320), wherein the reaction generates the heat required to spall the barrier, sustaining the reaction.|D. Product Recovery and Permanent Storage|[0027] As the Passivation Layer (210) continuously spalls, the turbulent flow of the Activation Fluid (140) sweeps the fractured micro-flakes out of the reactor bed. The fluid stream enters a Continuous Product Separator (410). The solid particulates are extracted as a Stable Mineral Slurry (420). The extracted mineral solids represent Permanent Carbon Sequestration (430); the CO2 is chemically bound in a thermodynamically stable state possessing a formation free energy of ΔGformation = -1012 kJ/mol.|E. Detailed Description of Drawings|[0028] Referring to FIG. 1, the physical reactor architecture is illustrated. The Insulated Reactor Vessel (110) houses the Packed Mineral Bed (120) containing the Magnesium-Silicate Substrate Particles (121). The Fluid Circulation System (130) injects the Activation Fluid (140) via the Fluid Injection Port (131) and removes it via the Fluid Effluent Port (132), extracting the mineralized products via the Continuous Product Separator (410), which outputs the Stable Mineral Slurry (420) and achieves Permanent Carbon Sequestration (430).|[0029] Referring to FIG. 2, the thermomechanical physics are mapped. The Unreacted Silicate Core (220) expands, creating Core Thermal Expansion Vectors (221), which outpace the Shell Thermal Expansion Vectors (211) of the Passivation Layer (210) due to the Exothermic Reaction Heat (230). This generates the Differential Thermal Strain (240) that triggers Spontaneous Thermal Fracture (250).|[0030] Referring to FIG. 3, the reaction kinetics are depicted along the Time Axis (710) and Carbonation Rate Axis (720). The graph contrasts a Passivated Carbonation Rate Curve (730) against a Sustained Thermomechanical Rate Curve (740), highlighting Fracture Event Triggers (750) that sustain high-volume throughput.|[0031] Referring to FIG. 4, the control logic is graphed. The Thermal Mismatch Controller (310) utilizes the Distributed Temperature Sensor Array (311), Feedback Signal Pathway (313), and Control Logic Circuit (312) to issue the Pump Control Signal (314) to the Variable Frequency Drive Pump (135), modulating fluid flow to maintain the Thermomechanical Depassivation Cycle (320).|F. List of Reference Numerals|[0032] The following reference numerals correspond to the structural elements illustrated in the accompanying drawings:|* (110) Insulated Reactor Vessel|* (120) Packed Mineral Bed|* (121) Magnesium-Silicate Substrate Particles|* (130) Fluid Circulation System|* (131) Fluid Injection Port|* (132) Fluid Effluent Port|* (135) Variable Frequency Drive Pump|* (140) Activation Fluid|* (210) Passivation Layer|* (211) Shell Thermal Expansion Vectors|* (220) Unreacted Silicate Core|* (221) Core Thermal Expansion Vectors|* (230) Exothermic Reaction Heat|* (240) Differential Thermal Strain|* (250) Spontaneous Thermal Fracture|* (310) Thermal Mismatch Controller|* (311) Distributed Temperature Sensor Array|* (312) Control Logic Circuit|* (313) Feedback Signal Pathway|* (314) Pump Control Signal|* (320) Thermomechanical Depassivation Cycle|* (410) Continuous Product Separator|* (420) Stable Mineral Slurry|* (430) Permanent Carbon Sequestration|* (710) Time Axis|* (720) Carbonation Rate Axis|* (730) Passivated Carbonation Rate Curve|* (740) Sustained Thermomechanical Rate Curve|* (750) Fracture Event Triggers|Best Mode and Manufacturing Method|[0033] The optimal physical execution utilizes standard mineral processing infrastructure. The Packed Mineral Bed (120) utilizes crushed uncalcined Olivine or Serpentinite to achieve a 50 to 500 µm particle diameter. The Insulated Reactor Vessel (110) is constructed from epoxy-coated carbon steel wrapped in industrial mineral wool to strictly restrict convective heat loss, operating at an internal pressure of 1.0 to 10.0 atm.|[0034] The Thermal Mismatch Controller (310) is instantiated via a Programmable Logic Controller (PLC) utilizing an explicitly defined computational architecture. The procedural logic operates at a 10 Hz sampling rate, executing a moving average filter to normalize input noise from the Distributed Temperature Sensor Array (311) consisting of K-type thermocouples inserted directly into the mineral bed. The baseline boundary condition assumes an ambient fluid temperature of 80°C. The Control Logic Circuit (312) calculates the instantaneous localized thermal anomaly (ΔT) and mathematically derives the induced thermal stress utilizing the exact formula σ = E · Δα · ΔT. The control loop utilizes hard numerical threshold criteria: if the calculated stress σ evaluates to less than 2.0 MPa, the controller automatically transmits a digital Pump Control Signal (314) to the Variable Frequency Drive Pump (135) to reduce the volumetric flow rate of the Activation Fluid (140) by 15% increments. This step-by-step restriction of convective cooling is maintained until the predefined thermal fracture threshold of 3.5 MPa is forcefully breached, actuating the Spontaneous Thermal Fracture (250).|Industrial Applicability and Regulatory Compliances|[0035] The invention provides direct industrial applicability in the Carbon Capture, Utilization, and Storage (CCUS) sector, specifically for operators seeking permanent mineral sequestration of emitted CO2 without the prohibitive energy costs associated with ultra-fine milling or high-pressure autoclaving. By utilizing low-pressure reactors and coarse mineral substrates, the apparatus complies with standard industrial pressure vessel regulations while outputting a thermodynamically stable solid carbonate that meets global environmental standards for permanent greenhouse gas storage and verifiable carbon crediting protocols. (IN202641043067)|Field of the Invention|[0001] The present invention relates generally to carbon dioxide sequestration, industrial chemical reactors, and geochemical processing. More specifically, the invention relates to a continuous mineral carbonation apparatus that exploits the exothermic heat of reaction to physically fracture a forming carbonate passivation layer. By thermally isolating a packed bed of silicate minerals and circulating an acidic, CO2-bearing fluid, the apparatus induces a localized temperature rise at the reaction front. By utilizing the differential coefficient of thermal expansion between the unreacted silicate substrate and the forming carbonate product layer, the system generates sufficient mechanical strain to continuously spall the barrier, sustaining carbon mineralization without requiring high-pressure autoclaves or external mechanical agitation. The invention defines a specific reactor architecture that deliberately accumulates exothermic reaction heat to exceed a defined fracture threshold to actuate a controlled mechanical depassivation mechanism.|Background of the Invention|[0002] Global mitigation of anthropogenic climate change involves the permanent sequestration of carbon dioxide (CO2). Mineral carbonation-reacting CO2 with magnesium- or calcium-rich silicate rocks to form stable solid carbonates-is a method of permanent carbon storage possessing minimal risk of atmospheric leakage. However, industrial-scale mineral carbonation is limited by surface passivation. As the carbonation reaction proceeds, the resulting solid carbonate and amorphous silica precipitate directly onto the surface of the unreacted silicate particle. This product layer forms an impermeable barrier that blocks further CO2 and water from accessing the unreacted core, causing the reaction rate to drop and stalling the process.|[0003] Mitigation solutions in the prior art rely on external continuous depassivation methods. These include grinding the rock to ultra-fine powders (< 10 µm) which incurs substantial additional energy requirements, processing the slurry in titanium-lined autoclaves at elevated temperatures and pressures (e.g., 150°C and 150 atm), or utilizing continuous mechanical attrition milling. Concurrently, industrial operations generate significant volumes of hot, acidic, highly saline waste fluid containing dissolved CO2. Operators allocate substantial resources treating and reinjecting this fluid.|[0004] An apparatus is required that addresses surface passivation without requiring continuous external mechanical or chemical energy inputs. The carbonation of silicate minerals such as Olivine is highly exothermic (ΔH = -89 kJ/mol). If a reactor isolates this heat at the particle interface, the localized temperature spike exploits the differing thermal expansion coefficients between the silicate core and the carbonate shell. The accumulated heat generates mechanical stress to continuously fracture and spall the passivation layer, yielding a continuous low-pressure reactor capable of permanent carbon mineralization.|Technical Problem and Solution|[0005] Core Technical Problem: Industrial processes react carbon dioxide with crushed silicate rock to transform the gas into solid mineral states. As the gas converts into a solid carbonate on the surface of the rock particle, it creates a passivation shell. This shell blocks the remaining gas from reaching the interior of the rock, halting the reaction. To break this shell, prior art industrial plants use energy-intensive crushers to grind the rock into microscopic dust or use high-pressure vessels to force the gas through the shell. These external methods consume substantial electrical energy.|[0006] Proposed Technical Solution: The present invention minimizes the reliance on external crushers or high-pressure vessels by utilizing an engineered reactor design that forces the rock to fracture its own passivation shell. The reaction between CO2 and the silicate rock releases a significant amount of heat. The invention utilizes an insulated reactor tank to trap this heat where the shell is forming, while actively controlling the flow of fluid to ensure the heat builds up to a predefined breaking point. The newly formed carbonate shell and the original rock core expand at different rates when heated. The trapped heat causes the core to expand faster than the shell, creating internal stress that shatters and flakes off the shell. This exposes fresh rock, which reacts with more gas, generating more heat to shatter the next layer in a continuous thermomechanical cycle.|Objects of the Invention|[0007] The primary object of the invention is to provide a mineral carbonation apparatus that executes continuous carbon sequestration without requiring external mechanical attrition or high-pressure autoclaves.|[0008] Another object is to physically exploit the exothermic heat of reaction as a mechanical fracture mechanism. By thermally isolating a packed reactor bed, the apparatus harnesses the enthalpy of carbonation to generate a localized ΔT of 15°C to 50°C at the solid-liquid reaction front.|[0009] A further object is to utilize differential thermal expansion for continuous, controlled depassivation. The apparatus relies on the structural mismatch between the Coefficient of Thermal Expansion (CTE) of the unreacted silicate substrate (α ≈ 12.4 x 10^-6 K^-1) and the precipitating carbonate passivation layer (α ≈ 9.5 x 10^-6 K^-1). The resulting thermal strain is accumulated to intentionally exceed the tensile strength of the carbonate layer, where the predefined thermal fracture threshold corresponds to a stress range of approximately 2 to 5 MPa, forcing the layer to crack and spall.|[0010] A still further object is to establish a thermomechanical depassivation cycle. As the passivation layer spalls, fresh silicate surface is exposed, increasing the carbonation rate. This increased rate generates additional exothermic heat, driving further thermal mismatch and spalling.|[0011] A final object is to valorize industrial wastewater. The apparatus comprises a fluid circulation system configured to accept hot, acidic, CO2-laden water from industrial operations. The low pH accelerates proton-promoted silicate dissolution, while the elevated fluid temperature lowers the required activation energy.|Summary of the Invention|[0012] The present invention discloses a carbon mineralization architecture that harnesses the thermodynamic waste heat of silicate carbonation to continuously destroy its reaction-limiting passivation barrier through a closed-loop flow control system.|[0013] The apparatus comprises an Insulated Reactor Vessel housing a Packed Mineral Bed consisting of coarsely crushed magnesium-silicate rock with a particle size ranging from 50 to 500 µm. A Fluid Circulation System continuously flows an acidic, CO2-saturated Activation Fluid through the packed bed.|[0014] As the CO2 reacts with the silicate, a Passivation Layer of solid carbonate and silica precipitates onto the particles. Simultaneously, the Exothermic Reaction Heat elevates the temperature at the particle-fluid interface. Due to the Differential Thermal Expansion between the silicate core and the carbonate shell, significant interfacial shear stress is generated. A Thermal Mismatch Controller modulates the fluid flow to ensure the localized heat accumulation intentionally exceeds a predefined Thermal Fracture Threshold of the passivation layer. This flow modulation is utilized specifically to induce thermomechanical failure of the passivation layer.|[0015] The layer undergoes Spontaneous Thermal Fracture and spalls off into the fluid stream as suspended particulate, continuously exposing fresh reactive surface. The fluid stream carries the solid carbonate products out of the reactor to a separation unit, yielding geologically stable CO2 sequestration alongside mineral aggregate.|Brief Description of the Accompanying Drawings|[0016] FIG. 1 is a structural and thermodynamic schematic illustrating the insulated reactor vessel, the packed mineral bed, and the fluid circulation system, including the outputs for the stable mineral slurry and permanent carbon sequestration.|[0017] FIG. 2 illustrates the Exothermic Differential-Expansion Physics, detailing the formation of the passivation layer, the localized heat generation, and the resulting thermal strain that causes engineered spalling.|[0018] FIG. 3 provides a graphical representation of the Reaction Rate Kinetics along defined axes, contrasting the decline of a passivated system against the sustained carbonation rate of the present apparatus.|[0019] FIG. 4 depicts the Thermomechanical Depassivation Control Logic, showing how the Thermal Mismatch Controller modulates fluid flow to maintain the critical fracture temperature.|Detailed Description of the Invention|A. Hardware Architecture and Mineral Processing|[0020] The core system comprises an Insulated Reactor Vessel (110) constructed of industrial alloys or composite liners, rated for continuous low-pressure operation in the range of 1 to 10 atm. The vessel houses a Packed Mineral Bed (120) comprising magnesium-rich silicate minerals in the form of Magnesium-Silicate Substrate Particles (121). The minerals are comminuted to a coarse particle size bounded strictly between 50 µm and 500 µm, establishing sufficient interstitial void space for fluid percolation.|[0021] A Fluid Circulation System (130) drives an Activation Fluid (140) through the bed. The Fluid Circulation System (130) routes fluid into the vessel via a Fluid Injection Port (131) and extracts it via a Fluid Effluent Port (132). The fluid is heavily doped with CO2 to achieve an acidic state bounded between pH 3.5 and 6.0. The Activation Fluid comprises aqueous streams heated to temperatures between 60°C and 100°C.|B. Exothermic Passivation and Differential Expansion|[0022] As detailed in FIG. 2, the dissolved CO2 triggers dissolution of the silicate, precipitating a Passivation Layer (210) comprising solid carbonate and amorphous silica directly onto an Unreacted Silicate Core (220). The carbonation of the silicate material releases Exothermic Reaction Heat (230) quantified by an enthalpy of ΔH = -89 kJ/mol. Because the Insulated Reactor Vessel (110) restricts thermal dissipation, this heat creates a localized ΔT of 15°C to 50°C directly at the reaction front.|[0023] The Unreacted Silicate Core possesses a Coefficient of Thermal Expansion (CTE) of α ≈ 12.4 x 10^-6 K^-1, while the Passivation Layer possesses a lower CTE of α ≈ 9.5 x 10^-6 K^-1. The Core Thermal Expansion Vectors (221) drastically exceed the Shell Thermal Expansion Vectors (211), creating interfacial shear. The localized ΔT induces severe Differential Thermal Strain (240) determined mathematically by the equation ε = Δα · ΔT.|[0024] The resulting thermal stress (σ = E · ε) is forced to accumulate to a level sufficient to cause the induced differential thermal strain to intentionally exceed a predefined thermal fracture threshold corresponding to a mathematically calculated mechanical stress range of 2 MPa to 5 MPa. This engineered internal shear stress forces the layer to undergo Spontaneous Thermal Fracture (250), spalling the barrier away from the core.|C. Thermodynamic Control and Cycle Maintenance|[0025] The apparatus utilizes a Thermal Mismatch Controller (310) which continuously monitors the internal temperature gradient via a Distributed Temperature Sensor Array (311). As graphed in FIG. 4, the Distributed Temperature Sensor Array (311) transmits data via a Feedback Signal Pathway (313) to a Control Logic Circuit (312). If the temperature at the reaction front drops, the thermal strain becomes insufficient to fracture the passivation layer. The controller outputs a Pump Control Signal (314) to a Variable Frequency Drive Pump (135) to reduce the volumetric flow rate of the Activation Fluid (140). This reduces convective heat loss (Qloss), forcing the Exothermic Reaction Heat (230) to accumulate locally until it breaches the critical predefined thermal fracture threshold.|[0026] Once fracture occurs, the exposure of fresh silicate triggers a spike in carbonation, generating new heat. This establishes a continuous Thermomechanical Depassivation Cycle (320), wherein the reaction generates the heat required to spall the barrier, sustaining the reaction.|D. Product Recovery and Permanent Storage|[0027] As the Passivation Layer (210) continuously spalls, the turbulent flow of the Activation Fluid (140) sweeps the fractured micro-flakes out of the reactor bed. The fluid stream enters a Continuous Product Separator (410). The solid particulates are extracted as a Stable Mineral Slurry (420). The extracted mineral solids represent Permanent Carbon Sequestration (430); the CO2 is chemically bound in a thermodynamically stable state possessing a formation free energy of ΔGformation = -1012 kJ/mol.|E. Detailed Description of Drawings|[0028] Referring to FIG. 1, the physical reactor architecture is illustrated. The Insulated Reactor Vessel (110) houses the Packed Mineral Bed (120) containing the Magnesium-Silicate Substrate Particles (121). The Fluid Circulation System (130) injects the Activation Fluid (140) via the Fluid Injection Port (131) and removes it via the Fluid Effluent Port (132), extracting the mineralized products via the Continuous Product Separator (410), which outputs the Stable Mineral Slurry (420) and achieves Permanent Carbon Sequestration (430).|[0029] Referring to FIG. 2, the thermomechanical physics are mapped. The Unreacted Silicate Core (220) expands, creating Core Thermal Expansion Vectors (221), which outpace the Shell Thermal Expansion Vectors (211) of the Passivation Layer (210) due to the Exothermic Reaction Heat (230). This generates the Differential Thermal Strain (240) that triggers Spontaneous Thermal Fracture (250).|[0030] Referring to FIG. 3, the reaction kinetics are depicted along the Time Axis (710) and Carbonation Rate Axis (720). The graph contrasts a Passivated Carbonation Rate Curve (730) against a Sustained Thermomechanical Rate Curve (740), highlighting Fracture Event Triggers (750) that sustain high-volume throughput.|[0031] Referring to FIG. 4, the control logic is graphed. The Thermal Mismatch Controller (310) utilizes the Distributed Temperature Sensor Array (311), Feedback Signal Pathway (313), and Control Logic Circuit (312) to issue the Pump Control Signal (314) to the Variable Frequency Drive Pump (135), modulating fluid flow to maintain the Thermomechanical Depassivation Cycle (320).|F. List of Reference Numerals|[0032] The following reference numerals correspond to the structural elements illustrated in the accompanying drawings:|* (110) Insulated Reactor Vessel|* (120) Packed Mineral Bed|* (121) Magnesium-Silicate Substrate Particles|* (130) Fluid Circulation System|* (131) Fluid Injection Port|* (132) Fluid Effluent Port|* (135) Variable Frequency Drive Pump|* (140) Activation Fluid|* (210) Passivation Layer|* (211) Shell Thermal Expansion Vectors|* (220) Unreacted Silicate Core|* (221) Core Thermal Expansion Vectors|* (230) Exothermic Reaction Heat|* (240) Differential Thermal Strain|* (250) Spontaneous Thermal Fracture|* (310) Thermal Mismatch Controller|* (311) Distributed Temperature Sensor Array|* (312) Control Logic Circuit|* (313) Feedback Signal Pathway|* (314) Pump Control Signal|* (320) Thermomechanical Depassivation Cycle|* (410) Continuous Product Separator|* (420) Stable Mineral Slurry|* (430) Permanent Carbon Sequestration|* (710) Time Axis|* (720) Carbonation Rate Axis|* (730) Passivated Carbonation Rate Curve|* (740) Sustained Thermomechanical Rate Curve|* (750) Fracture Event Triggers|Best Mode and Manufacturing Method|[0033] The optimal physical execution utilizes standard mineral processing infrastructure. The Packed Mineral Bed (120) utilizes crushed uncalcined Olivine or Serpentinite to achieve a 50 to 500 µm particle diameter. The Insulated Reactor Vessel (110) is constructed from epoxy-coated carbon steel wrapped in industrial mineral wool to strictly restrict convective heat loss, operating at an internal pressure of 1.0 to 10.0 atm.|[0034] The Thermal Mismatch Controller (310) is instantiated via a Programmable Logic Controller (PLC) utilizing an explicitly defined computational architecture. The procedural logic operates at a 10 Hz sampling rate, executing a moving average filter to normalize input noise from the Distributed Temperature Sensor Array (311) consisting of K-type thermocouples inserted directly into the mineral bed. The baseline boundary condition assumes an ambient fluid temperature of 80°C. The Control Logic Circuit (312) calculates the instantaneous localized thermal anomaly (ΔT) and mathematically derives the induced thermal stress utilizing the exact formula σ = E · Δα · ΔT. The control loop utilizes hard numerical threshold criteria: if the calculated stress σ evaluates to less than 2.0 MPa, the controller automatically transmits a digital Pump Control Signal (314) to the Variable Frequency Drive Pump (135) to reduce the volumetric flow rate of the Activation Fluid (140) by 15% increments. This step-by-step restriction of convective cooling is maintained until the predefined thermal fracture threshold of 3.5 MPa is forcefully breached, actuating the Spontaneous Thermal Fracture (250).|Industrial Applicability and Regulatory Compliances|[0035] The invention provides direct industrial applicability in the Carbon Capture, Utilization, and Storage (CCUS) sector, specifically for operators seeking permanent mineral sequestration of emitted CO2 without the prohibitive energy costs associated with ultra-fine milling or high-pressure autoclaving. By utilizing low-pressure reactors and coarse mineral substrates, the apparatus complies with standard industrial pressure vessel regulations while outputting a thermodynamically stable solid carbonate that meets global environmental standards for permanent greenhouse gas storage and verifiable carbon crediting protocols. Family Number|(118508361)|118508361|Abstract|(IN202641043067 A)|The invention relates to a continuous mineral carbonation apparatus that solves the problem of reaction-limiting surface passivation without mechanical attrition. The apparatus comprises an insulated reactor vessel (110) containing a packed mineral bed (120) of crushed magnesium-silicate substrate particles (121). A fluid circulation system (130) flows a CO2-saturated acidic activation fluid (140) through the bed. The resulting exothermic carbonation precipitates a solid carbonate passivation layer (210) on an unreacted silicate core (220), generating localized exothermic reaction heat (230). A thermal mismatch controller (310) restricts fluid flow, ensuring the heat accumulates to exceed a predefined thermal fracture threshold of the shell. Differential thermal expansion induces severe differential thermal strain (240), causing spontaneous thermal fracture (250) of the layer. A continuous product separator (410) extracts the spalled carbonate fragments as a stable mineral slurry (420), providing continuous permanent carbon dioxide sequestration (430).|IPC codes|(IN202641043067 A)|C01B-031/02|C01B-031/30|C01B-031/36|C01B-032/05| Materials, metallurgy C01B-031/02|C01B-031/30|C01B-031/36|C01B-032/05|C22B-034/12 C01B-031/02|C01B-031/30|C01B-031/36|C01B-032/05|C22B-034/12 PENDING (IN202641043067)|PENDING ALIVE (IN202641043067)|ALIVE (IN202641043067)|LEGAL DETAILS FOR IN202641043067|Actual or expected expiration date=2046-04-03|Legal state=ALIVE|Status=PENDING|Event publication date=2026-04-03|Event code=IN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=IN IN202641043067|Application date=2026-04-03|Standardized application number=2026IN-41043067|Event publication date=2026-04-10|Event code=IN/A|Event indicator=Pos|Event group=Examination events|Application laid open|Publication country=IN|Publication number=IN202641043067|Publication stage code=A|Publication date=2026-04-10|Standardized publication number=IN202641043067 (IN202641043067)|IN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=/WizbbSQlgu1TIIq3AdTyfLGbQMX8aAYa/WZFbsCsqzB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=IN0000000001759813&ekey=2304&xpn=IN202641043067&kind=A https://iprsearch.ipindia.gov.in/PublicSearch/PublicationSearch/ApplicationStatus https://permalink.orbit.com/RenderStaticFirstPage?XPN=KorjgOarj5Kw3D7frKnwocExnvIz5kLrfqHome9U%252B8A%3D%26n%3D1&id=0&base=FAMPAT IN (IN202641043067)|NAME=Babu Bapatla Surendra|NAME=Priyanka Irukumalli 0 1 Titre: (IN202641043067)|Mineral carbonation apparatus exploiting exothermic differential strain for continuous thermomechanical depassivation Résumé: (IN202641043067)|The invention relates to a continuous mineral carbonation apparatus that solves the problem of reaction-limiting surface passivation without mechanical attrition. The apparatus comprises an insulated reactor vessel (110) containing a packed mineral bed (120) of crushed magnesium-silicate substrate particles (121). A fluid circulation system (130) flows a CO2-saturated acidic activation fluid (140) through the bed. The resulting exothermic carbonation precipitates a solid carbonate passivation layer (210) on an unreacted silicate core (220), generating localized exothermic reaction heat (230). A thermal mismatch controller (310) restricts fluid flow, ensuring the heat accumulates to exceed a predefined thermal fracture threshold of the shell. Differential thermal expansion induces severe differential thermal strain (240), causing spontaneous thermal fracture (250) of the layer. A continuous product separator (410) extracts the spalled carbonate fragments as a stable mineral slurry (420), providing continuous permanent carbon dioxide sequestration (430). 97 Abstract gpt-4o-mini yes The patent describes a continuous mineral carbonation process aimed at CO2 sequestration using silicate minerals, which aligns with the topic of enhanced weathering.
100 CN201110146445 CN201110146445 CN102285654|CN102285654 7517240 CN102285654 B 2013-09-04 [CN102285654B]|CN102285654 A 2011-12-21 [CN102285654] 2011-06-02 2011-06-02 2013-09-04|2011-12-21 (CN102285654B)|2013-09-04 (CN102285654)|2018-06-02 (CN102285654)|Production method of silicon wafer cutting blade material (CN102285654)|The invention relates to a production method of a silicon wafer cutting blade material. The production method of the silicon wafer cutting blade material uses high-purity green silicon carbide as the raw material and comprises the following steps: performing jaw crushing, screening, performing automatic circulation type wet ball milling and hydraulic cyclone classification, performing automatic overflow carbon removal, performing magnetic separation to automatically remove iron, performing alkali washing, cleaning, performing overflow classification under automatic control of a programmable logic controller (PLC), centrifuging to dewater, drying, mixing, performing fine screening and the like. The silicon carbide blade material prepared by the method has equiareal shape, sharp edges and high cutting capability; the blade material particles have large specific surface area and clean appearance and high suitability to cutting fluid such as polyethylene glycol; the product ground by automatic circulation type wet ball milling and cyclone classification has more equiareal shapes, good grain shape and high yield, and overgrinding can be avoided; and automatic magnetic separation is adopted to perform acid-free iron removal, thus the method has high efficiency, environmental friendliness and high degree of automation and is suitable for large-scale production. The product ground by the method has high particle size concentration degree and good grain shape, and better cutting effect can be realized. JIANGSU TAYAL PHOTOVOLTAIC AUXILIARY MATERIAL (CN102285654)|Jiangsu Tayal Photovoltaic Auxiliary Material Co., Ltd.|(CN102285654)|Jiangsu Tayal Photovoltaic Auxiliary Material Co., Ltd. WANG PENG|LI HONG|WANG YI (CN102285654)|WANG PENG|LI HONG|WANG YI|(CN102285654)|WANG PENG|LI HONG|WANG YI (CN102285654)|6. the product crushed by adopting the automatic system combining the wet ball mill and the hydrocyclone has the advantages of more equal volume, good sharpness and the like, and the defects of low yield, serious over-crushing and the like are avoided; the yield of the preparation method reaches more than 80 percent, the particle size distribution of the product ground by adopting the process is more uniform, the better wafer cutting effect can be achieved, and the yield (the granularity section suitable for cutting the wafer) of the common grinding process adopted in the industry is about 50 percent.|At present, the production and processing modes of domestic silicon carbide cutting edge materials mainly comprise the following modes: the jet mill crushing production process has the advantages that the produced products are more than 90% in equivalent shape and higher in yield, but the jet mill is low in overall yield, the produced particles are round in shape and poor in sharpness, and recessive cracks exist and are not beneficial to cutting; the production process of Raymond mill grinding has high yield, but low yield, less volume of the produced product, and the like, which only accounts for about 50 percent, more particles with shapes of needle, sheet and the like, low cutting efficiency and poor cutting durability; in the prior art, the traditional wet ball mill is adopted for crushing, although product particles are large in volume and good in sharpness, the yield is low, the over-crushing is serious, and in addition, the acid consumption of the existing acid pickling iron removal process is large, the economy is poor, the pollution is large, and the trend of environmental protection is not met. Disclosure of Invention The invention aims to provide a preparation method of blade material silicon carbide for silicon wafer linear cutting, which has the advantages of high automation, high yield, high environmental protection and low energy consumption, and the prepared silicon carbide micro powder has the advantages of concentrated granularity, multiple grades, good sharpness, high cleanliness, strong adaptability with cutting fluid, strong cutting capability and lower TTV of the cut wafer; the method has the advantages of high yield, high automation degree, small pollution, low energy consumption and good economic benefit, and is very suitable for the production method of the silicon wafer cutting edge material in large-scale production.| (CN102285654)|1. A production method of a silicon wafer cutting edge material is characterized by comprising the following steps:crushing raw materials, namely selecting green silicon carbide block materials with the purity of more than or equal to 98 percent to perform jaw crushing, and screening silicon carbide sand grains with the granularity of less than or equal to 3mm after crushing;secondly, wet ball milling and grinding, and hydraulic cyclone classification, wherein the silicon carbide sand grains obtained in the first step are subjected to wet ball milling and grinding, and the hydraulic cyclone classification is carried out to obtain silicon carbide powder slurry in a required particle size range;thirdly, automatically removing carbon through overflow, namely introducing the silicon carbide powder slurry obtained in the second step into automatic overflow carbon removal equipment, adjusting the mass concentration of the silicon carbide powder slurry to 30-50 wt%, adding 30-50 ml of flotation oil and 50-70 ml of water glass, fully stirring for 0.5-1 hour, and then overflowing to remove free carbon; the automatic carbon removing equipment comprises an overflow barrel which is vertically arranged, an air inlet valve is arranged at the lower end of the overflow barrel, the upper end of the overflow barrel is connected with a diaphragm pump through a pipeline, an outer overflow groove and an inner overflow groove are also arranged at the upper end of the overflow barrel, the outer overflow groove is arranged on the outer side of the wall of the overflow barrel, a water inlet pipe and a water outlet pipe are also connected to the wall of the overflow barrel, the inner overflow groove is arranged in the middle of the inner part of the overflow barrel, a connecting pipeline is arranged between the outer overflow groove and the inner overflow groove, and the connecting pipeline is also connected with;the fourth step of magnetic separation and iron removal, namely introducing the silicon carbide powder slurry obtained in the third step into magnetic separation equipment, and controlling the flow of the slurry to be 16m3/h～20m3H, removing iron-containing impurities by magnetic separation;step five, introducing the silicon carbide powder slurry obtained in the step four into a reaction tank, adding NaOH solution according to 10-25 wt% of the mass of the slurry, controlling the temperature of the reaction tank to be 40-50 ℃, and removing free silicon and silicon dioxide after fully reacting for 2-3 hours;sixthly, cleaning the surfaces of the particles, namely pulping, stirring and cleaning the dehydrated raw materials by adopting pure water with the conductivity of less than or equal to 10 mu s/cm for further removing metal ion impurities on the surfaces of the particles;seventhly, overflow classification, namely introducing the cleaned slurry into an automatic overflow classification device, setting a classification program and adjusting the concentration of the slurry according to different particle size classification requirements, and performing hydraulic overflow classification, wherein water for classification is pure water with the conductivity of less than or equal to 10 mu s/cm;step eight, centrifugal dehydration, namely performing centrifugal dehydration treatment on the slurry obtained in the step seven to ensure that the water content of the obtained powder is less than or equal to 10%;ninth step, drying the centrifugally dewatered powder to make the water content less than 0.05%;tenth step, mixing, namely feeding the dried powder with the same granularity section in different batches into a dry mixer for dry mixing for 1-2 hours;and step eleven, fine screening, namely fine screening the powder obtained in the step ten by using an ultrasonic vibration screen, and removing agglomerates and large-particle impurities to obtain the silicon wafer cutting edge material.| (CN102285654)|The invention relates to a production method of a silicon wafer cutting edge material.|The invention relates to the field of multi-line cutting, in particular to a preparation method of blade material silicon carbide for solar photovoltaic silicon wafer line cutting.| (CN102285654)|SILICON WAFER(100,24)|OVERFLOW BARREL(100,17)|CUTTING EDGE(100,15)|SILICON WAFER CUTTING EDGE(100,13)|PRODUCTION METHOD(100,6)|HYDRAULIC CYCLONE CLASSIFICATION(86,7)|OVERFLOW CLASSIFICATION(60,9)|SILICON CARBIDE POWDER SLURRY(58,15)|POWDER SLURRY(55,15)|CENTRIFUGALLY DEWATERED POWDER(54,3)|CENTRIFUGAL DEHYDRATION(51,4)|JAW CRUSHING(50,3)|HYDRAULIC OVERFLOW CLASSIFICATION(48,3)|AUTOMATIC OVERFLOW CLASSIFICATION(45,3)|RECESSIVE CRACK(45,1)|SILICON CARBIDE(44,41)|INNER OVERFLOW GROOVE(43,6)|OVERFLOW BARREL WALL(43,6)|FINE SCREENING(41,8)|CONCENTRATED GRANULARITY(40,1)|OUTER OVERFLOW GROOVE(39,6)|CLASSIFYING CYCLONE(39,1)|CLASSIFICATION(38,8)|GRADING IMPELLER(38,6)|MULTILINE CUTTING(38,1)|CENTRIFUGAL DEHYDRATION TREATMENT(37,3)|HYDROCYCLONE(33,9)|MAGNETIC SEPARATOR(33,6)|SILICON WAFER CUTTING BLADE(33,3)|ECONOMIC BENEFIT(33,1)|FLASH EVAPORATOR(32,4)|CUTTING CAPABILITY(32,3)|CUTTING DURABILITY(32,1)|WAFER CUTTING(32,1)|YIELD DEFECT(32,1)|CLEANED SLURRY(31,3)|SILICON CARBIDE SAND GRAIN(30,5)|DOMESTIC SILICON CARBIDE(30,1)|ADAPTABILITY(29,3)|WET BALL MILL(29,3)|CLASSIFICATION ROTOR(28,2)|MIDDLING DISCHARGE PORT(28,1)|PIPELINE(27,10)|CLOTH BAG COLLECTOR(27,3)|OVERFLOW GRANULARITY(27,3)|ACID PICKLING(27,1)|CRUSHING(26,7)|REACTION TANK(26,7)|AGGLOMERATE REMOVAL(26,3)|DISPERSING FAN BLADE REVOLUTION(26,3)|AUTOMATIC CIRCULATION(26,1)|ACID CONSUMPTION(25,1)|CLEANLINESS(25,1)|BALL MILLING(24,14)|FLOTATION OIL(24,4)|ALKALI WASHING(24,1)|IRON REMOVAL(23,8)|WET BALL MILLING(23,4)|JET MILL(23,2)|AUTOMATION(23,1)|ENVIRONMENTAL PROTECTION(22,4)|AUTOMATION DEGREE(22,2)|CONTAMINATION(22,1)|CUT WAFER(22,1)|GRANULARITY SECTION(21,5)|ULTRASONIC VIBRATION SCREEN(21,5)|AUTOMATIC CARBON(21,2)|AUTOMATIC MAGNETIC SEPARATION ADOPTION(21,1)|SLURRY(20,18)|SAND GRAIN(20,5)|GRANULARITY(20,3)|CLASSIFICATION CYLINDER(20,2)|ULTRASONIC VIBRATION SIEVE(20,2)|AUTOMATIC OVERFLOW CARBON REMOVAL(20,1)|ECONOMY(20,1)|DRIED POWDER(19,4)|DRY MIXER(19,4)|OVERFLOW CARBON REMOVAL EQUIPMENT(19,3)|VARIABLE FREQUENCY(19,3)|OVERFLOW CYLINDER(19,2)|AUTOMATIC IRON REMOVAL(19,1)|MAGNETIC SUBSTANCE DISCHARGE(19,1)|MAGNETIC SEPARATION(18,13)|SILICON CARBIDE GRANULARITY(18,3)|CLEAN APPEARANCE(18,2)|GRINDING BALL(18,2)|FEED INLET(17,12)|FEED HOLE(17,9)|ULTRASONIC VIBRATION(17,7)|BATCH(17,4)|FEED PORT(17,4)|CENTRALIZED GRANULARITY RANGE(17,2)|LINEAR CUTTING(17,2)|SILICON WAFER LINEAR CUTTING(17,2)|PARTICLE PRODUCTION(17,1)|DRY MIX(16,4)|IMPURITY(16,4)|EQUAL VOLUME(16,2)|PRODUCT PRODUCTION(16,2)|GRINDING(15,10)|ENERGY CONSUMPTION(15,2)|OVERFLOW BARREL END(15,2)|PRODUCT PARTICLE(15,2)|CLEANING INLET GAS INLET(15,1)|GRINDING(15,1)|NEEDLE(15,1)|OVERFLOW(14,5)|PURE WATER ADOPTION(14,3)|PURITY(14,3)|GRAIN SHAPE(14,1)|MULTILINE CUTTING FIELD(14,1)|SMALL POLLUTION(14,1)|STEP EIGHT(14,1)|SILICON CARBIDE MICRO POWDER(13,4)|BLADE MATERIAL SILICON CARBIDE(13,3)|INTERNAL DISPERSING FAN BLADE(13,3)|PARTICLE SIZE CLASSIFICATION REQUIREMENT(13,3)|STEP ELEVEN(13,3)|SIEVING(13,2)|WAFER(13,2)|PARTICLE SHAPE(13,1)|BLADE MATERIAL(12,8)|BALL MILL CYLINDER(12,4)|DIAPHRAGM PUMP(12,4)|WATER INFLOW(12,4)|AIR INDUCING PORT(12,3)|CENTRIFUGE(12,3)|METAL ION IMPURITY REMOVAL(12,3)|REMOVING FREE SILICON(12,3)|EQUAL SHAPE(12,1)|MAGNETIC SEPARATION EQUIPMENT(11,5)|GRANULARITY REQUIREMENT(11,4)|OVERFLOW BARREL UPPER END(11,4)|CUTTING FLUID(11,3)|DRYING CYLINDER AIR INLET(11,2)|BLADE MATERIAL PARTICLE(11,1)|WATER OUTLET PIPE(10,4)|CLASSIFYING IMPELLER REVOLUTION(10,1)|MICRO POWDER(9,9)|STIRRING ROD(9,7)|MASS CONCENTRATION(9,6)|WATER INLET PIPE(9,4)|CRUSHED RAW MATERIAL(9,3)|FREQUENCY CONVERSION DISCHARGE(9,3)|RAW MATERIAL DEHYDRATION(9,3)|TANGENTIAL DIRECTION(9,3)|POLYETHYLENE GLYCOL(9,2)|WATER CONTENT(8,7)|COARSE MATERIAL COLLECTION PORT(8,5)|AIR INLET VALVE(8,4)|LARGE PARTICLE IMPURITY(8,4)|SLURRY TANK(8,4)|SODIUM HYDROXIDE SOLUTION(8,4)|CARBON COLLECTING POOL(8,3)|ROTATING SPEED(8,3)|ACID FREE IRON REMOVAL(8,1)|HYDROCYCLONE CLASSIFIER(8,1)|PLC AUTOMATIC CONTROL(8,1)|REMOVAL(8,1)|CUTTING BLADE MATERIAL(7,2)|MASS PRODUCTION(7,2)|CM PURE WATER(7,1)|OVERFLOW BARREL MIDDLE(7,1)|SHARP EDGE(7,1)|SODIUM HYDROXIDE(6,5)|PHOTOVOLTAIC LINEAR CUTTING(6,2)|CLASSIFYING ROTOR(6,1)|DOMESTIC ENTERPRISE(6,1)|MARKET COMPETITIVENESS(6,1)|PROCESSING MODE(6,1)|SILICON WAFER LINE CUTTING(6,1)|WATER PUMP(5,9)|PURE WATER(5,6)|SILICON CARBIDE BLADE MATERIAL(5,5)|INNER OVERFLOW(5,4)|PLC CONTROL UNIT(5,4)|WATER GLASS(5,4)|BLOCK MATERIAL(5,3)|HOT AIR INLET(5,3)|MEDIUM BALL WEIGHT RATIO(5,3)|ROTATIONAL FLOW DISCHARGE(5,3)|SILICON CARBIDE BLOCK MATERIAL(5,3)|1200 MESH SLURRY(5,1)|AUTOMATIC DECARBONIZATION EQUIPMENT(5,1)|CLASSIFICATION CIRCULATION(5,1)|EMISSION POLLUTION(5,1)|FOREIGN COUNTRY(5,1)|FUNDAMENTAL GUARANTEE(5,1)|HYDRAULIC CYCLONE CLASSIFIER(5,1)|HYDROCYCLONE FEEDING HOLE(5,1)|OVERFLOW BUCKET(5,1)|OVERFLOW CHUTE(5,1)|PRESET DEVICE CLASSIFICATION(5,1)|PURITY DEFECT(5,1)|UNEVEN GRANULARITY(5,1)|HIGH YIELD(4,5)|OUTER OVERFLOW(4,3)|REMOVING CARBON(4,3)|HEAVY METAL TOTAL CONTENT(4,2)|1000 MESH SLURRY(4,1)|ABSOLUTE MARKET(4,1)|ALKALINE WASH(4,1)|CLEAN SLURRY(4,1)|COARSE PARTICLE(4,1)|DISCHARGING HOLE CYLINDER(4,1)|GRINDING REQUIREMENT RETURN(4,1)|LINE CUTTING(4,1)|MIDDLING DISCHARGE HOLE(4,1)|ONLY ACCOUNT(4,1)|SOLAR PHOTOVOLTAIC INDUSTRY(4,1)|AUTOMATIC CARBON REMOVAL(3,2)|CUTTING EDGE MATERIAL(3,2)|ELECTRICAL CONTROL VALVE(3,2)|FLASH EVAPORATION MACHINE(3,2)|METALLIC IMPURITY(3,2)||(CN102285654)|SILICON WAFER(100,26)|CUTTING EDGE(100,14)|SILICON WAFER CUTTING EDGE(100,12)|PRODUCTION METHOD(100,5)|HYDRAULIC CYCLONE CLASSIFICATION(99,7)|OVERFLOW CLASSIFICATION(69,9)|SILICON CARBIDE POWDER SLURRY(67,15)|POWDER SLURRY(63,15)|CENTRIFUGALLY DEWATERED POWDER(62,3)|CENTRIFUGAL DEHYDRATION(59,4)|JAW CRUSHING(57,3)|HYDRAULIC OVERFLOW CLASSIFICATION(55,3)|AUTOMATIC OVERFLOW CLASSIFICATION(52,3)|SILICON CARBIDE(48,41)|FINE SCREENING(48,8)|CONCENTRATED GRANULARITY(46,1)|CLASSIFYING CYCLONE(45,1)|SILICON WAFER CUTTING BLADE(44,4)|MULTILINE CUTTING(44,1)|GRADING IMPELLER(43,6)|CENTRIFUGAL DEHYDRATION TREATMENT(43,3)|INNER OVERFLOW TANK(40,3)|HYDROCYCLONE(38,9)|MAGNETIC SEPARATOR(38,6)|ECONOMIC BENEFIT(38,1)|CLASSIFICATION(37,6)|FLASH EVAPORATOR(37,4)|WAFER CUTTING(37,1)|YIELD DEFECT(37,1)|CUTTING CAPABILITY(36,3)|OUTER OVERFLOW TANK(36,3)|CLEANED SLURRY(35,3)|SILICON CARBIDE SAND GRAIN(34,5)|ADAPTABILITY(33,3)|CLASSIFICATION ROTOR(33,2)|MIDDLING DISCHARGE PORT(33,1)|CLOTH BAG COLLECTOR(32,3)|OVERFLOW GRANULARITY(31,3)|REACTION TANK(30,7)|AGGLOMERATE REMOVAL(30,3)|DISPERSING FAN BLADE REVOLUTION(30,3)|AUTOMATIC CIRCULATION(30,1)|SILICON CARBIDE GRANULARITY SAND(29,2)|CLEANLINESS(28,1)|BALL MILLING(27,14)|IRON REMOVAL(27,8)|FLOTATION OIL(27,4)|ALKALI WASHING(27,1)|SLURRY(26,22)|WET BALL MILLING(26,4)|AUTOMATION(26,1)|ULTRASONIC VIBRATION SCREEN(25,5)|AUTOMATION DEGREE(25,2)|CARBON RECOVERY TANK(25,1)|CUT WAFER(25,1)|GRANULARITY SECTION(24,5)|CLASSIFICATION CYLINDER(24,2)|ULTRASONIC VIBRATION SIEVE(24,2)|AUTOMATIC MAGNETIC SEPARATION ADOPTION(24,1)|CRUSHING(23,7)|SAND GRAIN(23,5)|CLASSIFICATION WATER(23,3)|GRANULARITY(23,3)|AUTOMATIC OVERFLOW CARBON REMOVAL(23,1)|DRIED POWDER(22,4)|DRY MIXER(22,4)|OVERFLOW CARBON REMOVAL EQUIPMENT(22,3)|OVERFLOW CYLINDER(22,2)|AUTOMATIC IRON REMOVAL(22,1)|MAGNETIC SUBSTANCE DISCHARGE(22,1)|MAGNETIC SEPARATION(21,13)|VARIABLE FREQUENCY(21,3)|CLEAN APPEARANCE(21,2)|GRINDING BALL(21,2)|PIPELINE(20,10)|BATCH(20,4)|FEED PORT(20,4)|WET BALL MILL(20,3)|FEED INLET(19,12)|FEED HOLE(19,9)|ULTRASONIC VIBRATION(19,7)|MEDIUM BALL(19,4)|CENTRALIZED GRANULARITY RANGE(19,2)|LINEAR CUTTING(19,2)|SILICON WAFER LINEAR CUTTING(19,2)|GRINDING RATIO(19,1)|DRY MIX(18,4)|ENVIRONMENTAL PROTECTION(18,4)|IMPURITY(18,4)|ENERGY CONSUMPTION(18,2)|EQUAL VOLUME(18,2)|CLEANING INLET GAS INLET(18,1)|GRINDING(18,1)|CUTTING BLADE MATERIAL(17,4)|PURITY(17,3)|GRAIN SHAPE(17,1)|MULTILINE CUTTING FIELD(17,1)|SMALL POLLUTION(17,1)|STEP EIGHT(17,1)|OVERFLOW(16,5)|SILICON CARBIDE MICRO POWDER(16,4)|PURE WATER ADOPTION(16,3)|STEP ELEVEN(16,3)|PARTICLE SHAPE(16,1)|BLADE MATERIAL SILICON CARBIDE(15,3)|INTERNAL DISPERSING FAN BLADE(15,3)|PARTICLE SIZE CLASSIFICATION REQUIREMENT(15,3)|SIEVING(15,2)|WAFER(15,2)|BLADE MATERIAL(14,8)|AIR INDUCING PORT(14,3)|BALL MILL CYLINDER(14,3)|CENTRIFUGE(14,3)|METAL ION IMPURITY REMOVAL(14,3)|REMOVING FREE SILICON(14,3)|MAGNETIC SEPARATION EQUIPMENT(13,5)|SODIUM HYDROXIDE SOLUTION(13,5)|WATER INFLOW(13,4)|DRYING CYLINDER AIR INLET(13,2)|AUTOMATIC CARBON REMOVAL EQUIPMENT(13,1)|GRANULARITY REQUIREMENT(12,4)|CUTTING FLUID(12,3)|BLADE MATERIAL PARTICLE(12,1)|MASS CONCENTRATION(11,6)|FREQUENCY CONVERSION DISCHARGE(11,3)|RAW MATERIAL DEHYDRATION(11,3)|CLASSIFYING IMPELLER REVOLUTION(11,1)|MICRO POWDER(10,9)|STIRRING ROD(10,7)|WATER CONTENT(10,7)|LARGE PARTICLE IMPURITY(10,4)|OVERFLOW BARREL WALL(10,4)|CRUSHED RAW MATERIAL(10,3)|TANGENTIAL DIRECTION(10,3)|POLYETHYLENE GLYCOL(10,2)|ELECTRIC CONDUCTIVITY(10,1)|SODIUM HYDROXIDE(9,6)|COARSE MATERIAL COLLECTION PORT(9,5)|DIAPHRAGM PUMP(9,4)|SLURRY TANK(9,4)|CARBON COLLECTING POOL(9,3)|ROTATING SPEED(9,3)|ACID FREE IRON REMOVAL(9,1)|HYDROCYCLONE CLASSIFIER(9,1)|PLC AUTOMATIC CONTROL(9,1)|PURE WATER(8,7)|WATER OUTLET PIPE(8,4)|MASS PRODUCTION(8,2)|OVERFLOW BARREL MIDDLE(8,1)|SHARP EDGE(8,1)|INNER OVERFLOW GROOVE(7,3)|PHOTOVOLTAIC LINEAR CUTTING(7,2)|CLASSIFYING ROTOR(7,1)|DOMESTIC ENTERPRISE(7,1)|MARKET COMPETITIVENESS(7,1)|SILICON WAFER LINE CUTTING(7,1)|WATER PUMP(6,9)|SILICON CARBIDE BLADE MATERIAL(6,5)|AIR INLET VALVE(6,4)|PLC CONTROL UNIT(6,4)|WATER GLASS(6,4)|BLOCK MATERIAL(6,3)|HOT AIR INLET(6,3)|ROTATIONAL FLOW DISCHARGE(6,3)|SILICON CARBIDE BLOCK MATERIAL(6,3)|WEIGHT RATIO(6,3)|AUTOMATIC DECARBONIZATION EQUIPMENT(6,1)|CLASSIFICATION CIRCULATION(6,1)|EMISSION POLLUTION(6,1)|FOREIGN COUNTRY(6,1)|FUNDAMENTAL GUARANTEE(6,1)|HYDRAULIC CYCLONE CLASSIFIER(6,1)|HYDROCYCLONE FEEDING HOLE(6,1)|OVERFLOW BUCKET(6,1)|OVERFLOW CHUTE(6,1)|PRESET DEVICE CLASSIFICATION(6,1)|PURITY DEFECT(6,1)|RECESSIVE CRACK(6,1)|UNEVEN GRANULARITY(6,1)|OUTER OVERFLOW GROOVE(5,3)|HEAVY METAL TOTAL CONTENT(5,2)|ABSOLUTE MARKET(5,1)|ALKALINE WASH(5,1)|CLEAN SLURRY(5,1)|COARSE PARTICLE(5,1)|DISCHARGING HOLE CYLINDER(5,1)|GRINDING REQUIREMENT RETURN(5,1)|LINE CUTTING(5,1)|MIDDLING DISCHARGE HOLE(5,1)|SILICON CARBIDE GRANULARITY(5,1)|SOLAR PHOTOVOLTAIC INDUSTRY(5,1)|HOT AIR TEMPERATURE(4,3)|REMOVING CARBON(4,3)|ROTATION SPEED(4,3)|ELECTRICAL CONTROL VALVE(4,2)|FLASH EVAPORATION MACHINE(4,2)|METALLIC IMPURITY(4,2)|PRODUCT PARTICLE(4,2)|ACID PICKLING(4,1)|ADOPTED SCREEN(4,1)|BALL MILL BARREL(4,1)|COLLECTION TANK(4,1)|CUT SILICON WAFER TTV(4,1)|CUTTING DURABILITY(4,1)|CYCLONE CYLINDER WALL(4,1)| (CN102285654)|1. A production method of a silicon wafer cutting edge material is characterized by comprising the following steps:|crushing raw materials, namely selecting green silicon carbide block materials with the purity of more than or equal to 98 percent to perform jaw crushing, and screening silicon carbide sand grains with the granularity of less than or equal to 3mm after crushing;|secondly, wet ball milling and grinding, and hydraulic cyclone classification, wherein the silicon carbide sand grains obtained in the first step are subjected to wet ball milling and grinding, and the hydraulic cyclone classification is carried out to obtain silicon carbide powder slurry in a required particle size range;|thirdly, automatically removing carbon through overflow, namely introducing the silicon carbide powder slurry obtained in the second step into automatic overflow carbon removal equipment, adjusting the mass concentration of the silicon carbide powder slurry to 30-50 wt%, adding 30-50 ml of flotation oil and 50-70 ml of water glass, fully stirring for 0.5-1 hour, and then overflowing to remove free carbon; the automatic carbon removing equipment comprises an overflow barrel which is vertically arranged, an air inlet valve is arranged at the lower end of the overflow barrel, the upper end of the overflow barrel is connected with a diaphragm pump through a pipeline, an outer overflow groove and an inner overflow groove are also arranged at the upper end of the overflow barrel, the outer overflow groove is arranged on the outer side of the wall of the overflow barrel, a water inlet pipe and a water outlet pipe are also connected to the wall of the overflow barrel, the inner overflow groove is arranged in the middle of the inner part of the overflow barrel, a connecting pipeline is arranged between the outer overflow groove and the inner overflow groove, and the connecting pipeline is also connected with;|the fourth step of magnetic separation and iron removal, namely introducing the silicon carbide powder slurry obtained in the third step into magnetic separation equipment, and controlling the flow of the slurry to be 16m3/h～20m3H, removing iron-containing impurities by magnetic separation;|step five, introducing the silicon carbide powder slurry obtained in the step four into a reaction tank, adding NaOH solution according to 10-25 wt% of the mass of the slurry, controlling the temperature of the reaction tank to be 40-50 ℃, and removing free silicon and silicon dioxide after fully reacting for 2-3 hours;|sixthly, cleaning the surfaces of the particles, namely pulping, stirring and cleaning the dehydrated raw materials by adopting pure water with the conductivity of less than or equal to 10 mu s/cm for further removing metal ion impurities on the surfaces of the particles;|seventhly, overflow classification, namely introducing the cleaned slurry into an automatic overflow classification device, setting a classification program and adjusting the concentration of the slurry according to different particle size classification requirements, and performing hydraulic overflow classification, wherein water for classification is pure water with the conductivity of less than or equal to 10 mu s/cm;|step eight, centrifugal dehydration, namely performing centrifugal dehydration treatment on the slurry obtained in the step seven to ensure that the water content of the obtained powder is less than or equal to 10%;|ninth step, drying the centrifugally dewatered powder to make the water content less than 0.05%;|tenth step, mixing, namely feeding the dried powder with the same granularity section in different batches into a dry mixer for dry mixing for 1-2 hours;|and step eleven, fine screening, namely fine screening the powder obtained in the step ten by using an ultrasonic vibration screen, and removing agglomerates and large-particle impurities to obtain the silicon wafer cutting edge material.|2. The method for producing the silicon wafer cutting blade material according to claim 1, wherein the wet ball milling in the second step is performed by using a vertical variable frequency wet ball mill, the vertical variable frequency wet ball mill comprises a vertical ball mill cylinder and a stirring rod arranged in the cylinder in a matching manner, the stirring rod is driven by a variable speed motor, a feed port is arranged at the lower part of the cylinder in the tangential direction, a discharge port is arranged at the upper part of the cylinder, and the discharge port is connected with the feed port of a hydrocyclone through a water pump; the middle upper part of the hydraulic cyclone is provided with a feed inlet, the upper part of the hydraulic cyclone is provided with a rotational flow discharge port, the lower part of the hydraulic cyclone is provided with a coarse material collecting port, and the feed inlet of the middle upper part is connected with a slurry tank for collecting the discharge of the vertical frequency conversion wet ball mill through a water pump.|3. The production method of the silicon wafer cutting edge material according to claim 2, wherein when the vertical frequency conversion wet ball mill and the hydrocyclone are used for grinding and grading, the medium balls are added according to the weight ratio of the medium balls to the silicon carbide granularity sand of 2-3.5: 1, the rotating speed of a ball grinding head of the vertical frequency conversion wet ball mill is 100-300 rpm, and the water inflow rate of the hydrocyclone is 100L/h-500L/h.|4. The method for producing a silicon wafer cutting blade material as claimed in claim 1, wherein the magnetic separator in said fourth step comprises a magnetic separator body and a PLC control unit, wherein a discharge port and a cleaning inlet gas inlet are provided in an upper part of said magnetic separator body, and a feed port, a middling discharge port and a magnetic substance discharge port are provided in a lower part thereof.|5. A method for the production of a silicon wafer cutting edge stock according to claim 1, characterized in that in the sixth step 6 a substrate is treated with a conductivity of less than 10 μ s-Repeatedly washing the dewatered material with cm pure water for more than 3 times to obtain Fe in the slurry2O3The mass percentage is less than 0.10 percent, and the total content of other heavy metals is less than 0.005 percent.|6. The method for producing the silicon wafer cutting blade material according to claim 1, wherein the automatic control overflow classification device in the seventh step comprises an overflow cylinder, a PLC control unit, an electric control valve and a flow sensor; and during overflow classification, controlling the inflow rate to be 500-1200L/h according to the overflow granularity, and enabling the mass concentration of the slurry to reach 15-25 wt% to obtain the slurry with the centralized granularity range.|7. The method for producing the silicon wafer cutting edge material according to claim 1, wherein in the eighth step, a centrifuge is used for concentration and dehydration, filter cloth of 500 to 2500 meshes is used, and the rotation speed of the centrifuge is 800 to 2500 rpm; in the tenth step, the energy gear of the ultrasonic vibration sieve is adjusted to be 50-80%, and the used sieve is 200-500 meshes.|8. The method for producing the silicon wafer cutting blade material according to claim 1, wherein in the ninth step, the drying is performed by a flash evaporator; the flash evaporator comprises a drying cylinder, a grading cylinder and a fine powder collecting device; the drying cylinder is provided with a hot air inlet and internal dispersing fan blades, and the dispersing fan blades are controlled by a variable speed motor; the grading cylinder comprises a feeding hole, a grading impeller and a discharging hole, the feeding hole is connected with the drying cylinder, and the grading impeller is controlled by a variable speed motor; the fine powder collecting device comprises an air inducing port and a cloth bag collector; the hot air temperature of the air inlet of the drying cylinder is controlled to be 200-300 ℃, and the revolution of the dispersing fan blades is 100-500 rpm; the revolution of the classification impeller in the classification cylinder is 500-1500 rpm. (CN102285654)|TECHNICAL FIELD|[0002] The invention relates to the field of multi-line cutting, in particular to a preparation method of blade material silicon carbide for solar photovoltaic silicon wafer line cutting.|BACKGROUND ART|[0004] With the rapid development of the solar photovoltaic industry, the demand for high quality silicon wafers is increasing day by day. The processing of silicon wafers is an important link in the manufacture of solar cell sets, and an effective silicon wafer cutting technology is a fundamental guarantee for obtaining high-quality silicon wafers. In recent years, the Multi-Wire Saw (Multi-Wire Saw) of the heterophoria has taken an absolute market lead in the field of large-size silicon wafer processing with its high yield and yield, and the mixed cutting agent-mortar used in the Multi-Wire cutting has an important role and plays a major role in the cutting process. The silicon carbide micro powder as a cutting edge material has wide application in the production field of solar silicon wafers and semiconductor wafers, and is an indispensable special cutting edge material in the production process of linear cutting of silicon wafers.|[0005] The prior art edge material for photovoltaic linear cutting in China has uneven quality, and has the defects of lower purity, uneven granularity, poor cutting efficiency and the like compared with the similar products in foreign countries. Domestic enterprises have backward production equipment and process, poor crushing effect, wide micro powder particle size distribution and lack of market competitiveness. At present, the production and processing modes of domestic silicon carbide cutting edge materials mainly comprise the following modes: the jet mill crushing production process has the advantages that the produced products are more than 90% in equivalent shape and higher in yield, but the jet mill is low in overall yield, the produced particles are round in shape and poor in sharpness, and recessive cracks exist and are not beneficial to cutting; the production process of Raymond mill grinding has high yield, but low yield, less volume of the produced product, and the like, which only accounts for about 50 percent, more particles with shapes of needle, sheet and the like, low cutting efficiency and poor cutting durability; in the prior art, the traditional wet ball mill is adopted for crushing, although product particles are large in volume and good in sharpness, the yield is low, the over-crushing is serious, and in addition, the acid consumption of the existing acid pickling iron removal process is large, the economy is poor, the pollution is large, and the trend of environmental protection is not met.|DISCLOSURE|[0006] Disclosure of Invention|[0007] The invention aims to provide a preparation method of blade material silicon carbide for silicon wafer linear cutting, which has the advantages of high automation, high yield, high environmental protection and low energy consumption, and the prepared silicon carbide micro powder has the advantages of concentrated granularity, multiple grades, good sharpness, high cleanliness, strong adaptability with cutting fluid, strong cutting capability and lower TTV of the cut wafer; the method has the advantages of high yield, high automation degree, small pollution, low energy consumption and good economic benefit, and is very suitable for the production method of the silicon wafer cutting edge material in large-scale production.|[0008] In order to solve the technical problems, the invention adopts the technical scheme that: a production method of a silicon wafer cutting edge material is characterized by comprising the following steps:|[0009] crushing raw materials, namely selecting green silicon carbide block materials with the purity of more than or equal to 98 percent to perform jaw crushing, and screening silicon carbide sand grains with the granularity of less than or equal to 3mm after crushing;|[0010] secondly, wet ball milling and grinding, and hydraulic cyclone classification, wherein the silicon carbide sand grains obtained in the first step are subjected to wet ball milling and grinding, and the hydraulic cyclone classification is carried out to obtain silicon carbide powder slurry in a required particle size range;|[0011] thirdly, automatically removing carbon through overflow, introducing the silicon carbide powder slurry obtained in the second step into automatic overflow carbon removal equipment, adjusting the mass concentration of the silicon carbide powder slurry to 30-50 wt%, adding 30-50 ml of flotation oil and 50-70 ml of water glass, fully stirring for 0.5-1 hour, and then overflowing to remove free carbon;|[0012] the fourth step of magnetic separation and iron removal, namely introducing the silicon carbide powder slurry obtained in the third step into magnetic separation equipment, and controlling the flow of the slurry to be 16m3/h～20m3H, removing iron-containing impurities by magnetic separation;|[0013] step five, introducing the silicon carbide powder slurry obtained in the step four into a reaction tank, adding NaOH solution according to 10-25 wt% of the mass of the slurry, controlling the temperature of the reaction tank to be 40-50 ℃, and removing free silicon and silicon dioxide after fully reacting for 2-3 hours;|[0014] sixthly, cleaning the surfaces of the particles, namely pulping, stirring and cleaning the dehydrated raw materials by adopting pure water with the conductivity of less than or equal to 10 mu s/cm for further removing metal ion impurities on the surfaces of the particles;|[0015] seventhly, overflow classification, namely introducing the cleaned slurry into an automatic overflow classification device, setting a classification program and adjusting the concentration of the slurry according to different particle size classification requirements, and performing hydraulic overflow classification, wherein the classification water is pure water with the conductivity of less than or equal to 10 us/cm;|[0016] step eight, centrifugal dehydration, namely performing centrifugal dehydration treatment on the slurry obtained in the step seven to ensure that the water content of the obtained powder is less than or equal to 10%;|[0017] ninth step, drying the centrifugally dewatered powder to make the water content less than 0.05%;|[0018] tenth step, mixing, namely feeding the dried powder with the same granularity section in different batches into a dry mixer for dry mixing for 1-2 hours;|[0019] and step eleven, fine screening, namely fine screening the powder obtained in the step ten by using an ultrasonic vibration screen, and removing agglomerates and large-particle impurities to obtain the silicon wafer cutting edge material.|[0020] The wet ball milling in the second step is carried out by selecting a vertical frequency conversion wet ball mill, the vertical frequency conversion wet ball mill comprises a vertical ball mill cylinder and a stirring rod arranged in the cylinder in a matching way, the stirring rod is driven by a variable speed motor, a feeding hole is arranged at the lower part of the cylinder along the tangential direction, a discharging hole is arranged at the upper part of the cylinder, and the discharging hole is connected with the feeding hole of the hydrocyclone through a water pump; the middle upper part of the hydraulic cyclone is provided with a feed inlet, the upper part of the hydraulic cyclone is provided with a rotational flow discharge port, the lower part of the hydraulic cyclone is provided with a coarse material collecting port, and the feed inlet of the middle upper part is connected with a slurry tank for collecting the discharge of the vertical frequency conversion wet ball mill through a water pump.|[0021] When the vertical frequency conversion wet ball mill and the hydrocyclone are used for grinding and grading, the medium balls are added according to the weight ratio of the medium balls to the silicon carbide granularity sand of 2-3.5: 1, the rotating speed of a ball grinding head of the vertical frequency conversion wet ball mill is 100-300 rpm, and the water inflow rate of the hydrocyclone is 100L/h-500L/h.|[0022] The automatic carbon removing equipment in the third step comprises an overflow barrel which is vertically arranged, an air inlet valve is arranged at the lower end of the overflow barrel, the upper end of the overflow barrel is connected with a diaphragm pump through a pipeline, an outer overflow groove and an inner overflow groove are further arranged at the upper end of the overflow barrel, the outer overflow groove is arranged on the outer side of the wall of the overflow barrel, a water inlet pipe and a water outlet pipe are further connected to the wall of the overflow barrel, the inner overflow groove is arranged in the middle of the overflow barrel, a connecting pipeline is arranged between the outer overflow groove and the inner overflow groove, and the connecting pipeline is further connected with a carbon collecting pool.|[0023] The magnetic separation equipment in the fourth step comprises a magnetic separator body and a PLC control unit, wherein a discharge hole and an air inlet for cleaning are formed in the upper portion of the magnetic separator body, and a feed inlet, a middling discharge hole and a magnetic material discharge hole are formed in the lower portion of the magnetic separator body.|[0024] The reagent used in said fifth step is aqueous NaOH solution.|[0025] In the sixth step 6, the dehydrated material is repeatedly washed 3 times or more with pure water having a conductivity of less than 10 μ s/cm to make Fe in the slurry2O3The mass percentage is less than 0.10 percent, and the total content of other heavy metals is less than 0.005 percent.|[0026] The automatic control overflow grading device in the seventh step comprises an overflow cylinder, a PLC control unit, an electric control valve and a flow sensor; and during overflow classification, controlling the inflow rate to be 500-1200L/h according to the overflow granularity, and enabling the mass concentration of the slurry to reach 15-25 wt% to obtain the slurry with the centralized granularity range.|[0027] In the eighth step, a centrifuge is adopted for concentration and dehydration, 500-2500-mesh filter cloth is adopted, and the rotation speed of the centrifuge is 800-2500 rpm; in the tenth step, the energy gear of the ultrasonic vibration sieve is adjusted to be 50-80%, and the used sieve is 200-500 meshes.|[0028] In the ninth step, the drying is carried out by adopting a flash evaporation machine; the flash evaporator comprises a drying cylinder, a grading cylinder and a fine powder collecting device; the drying cylinder is provided with a hot air inlet and internal dispersing fan blades, and the dispersing fan blades are controlled by a variable speed motor; the grading cylinder comprises a feeding hole, a grading impeller and a discharging hole, the feeding hole is connected with the drying cylinder, and the grading impeller is controlled by a variable speed motor; the fine powder collecting device comprises an air inducing port and a cloth bag collector; the hot air temperature of the air inlet of the drying cylinder is controlled to be 200-300 ℃, and the revolution of the dispersing fan blades is 100-500 rpm; the revolution of the classification impeller in the classification cylinder is 500-1500 rpm.|[0029] The invention has the positive and beneficial effects that:|[0030] 1. the silicon carbide blade material prepared by the invention is in an equal volume shape, and keeps a sharp edge angle (see figure 1), so that the balanced self-sharpening property of silicon carbide micro powder as a cutting blade material is ensured, the cutting capability is strong, the TTV of a cut silicon wafer is minimized, and the silicon carbide blade material has the characteristics of high hardness, strong wear resistance, good high-temperature resistance, high thermal conductivity and the like, and the performance indexes of the silicon carbide blade material are shown in table 1;|[0031] 2. the product particles have large specific surface area and clean appearance, and have strong adaptability with common cutting fluids such as polyethylene glycol and the like;|[0032] 3. pure water with the conductivity less than 10 mu s/cm is adopted to repeatedly elute the dehydrated material, so that the content of metal impurities in slurry is extremely low, the influence of the metal impurities on the wafer during the cutting of the semiconductor wafer is reduced, and the method plays an important role in improving the quality of the wafer;|[0033] 4. an overflow automatic carbon removal system is adopted, so that the yield is greatly improved, and the labor cost is reduced;|[0034] 5. an acid-free automatic iron removal system is adopted, so that the production cost of acid is greatly reduced, the emission pollution is reduced, and the concept of energy conservation and environmental protection is met;|[0035] 6. the product crushed by adopting the automatic system combining the wet ball mill and the hydrocyclone has the advantages of more equal volume, good sharpness and the like, and the defects of low yield, serious over-crushing and the like are avoided; the yield of the preparation method reaches more than 80 percent, the particle size distribution of the product ground by adopting the process is more uniform, the better wafer cutting effect can be achieved, and the yield (the granularity section suitable for cutting the wafer) of the common grinding process adopted in the industry is about 50 percent.|DRAWINGS DESCRIPTION|[0037] FIG. 1 is a scanning electron micrograph of a silicon wafer cutting edge material produced by the method of the present invention;|[0038] FIG. 2 is a schematic diagram of the structure of a wet ball mill modified in the method of the present invention;|[0039] FIG. 3 is a schematic diagram of the construction of a hydrocyclone used in the process of the present invention;|[0040] FIG. 4 is a schematic structural view of an automatic carbon removal apparatus used in the method of the present invention.|[0041] In fig. 2: 1. a variable speed motor; 2. a discharge port; 3. a stirring rod; 4. a rotating shaft; 5. a barrel; 6. a feed inlet; 7. a conical buffer transition section.|[0042] In fig. 3: 1. a fine material discharge port of the cyclone; 2. a feed inlet; 3. the discharge port is connected with the cylinder body through a valve; 4. a barrel; 5. a conical buffer transition section 6 and a coarse material discharge port.|[0043] In fig. 4: 1. an overflow bucket; 2 is an air inlet valve; 3. a diaphragm pump; 4. an overflow chute; 5. an inner overflow launder; 6. a water inlet pipe; 7. a water outlet pipe; 8. a pipeline; 9. a carbon collecting pool; 10. a connecting rod; 11. and (4) end covers.|INVENTION MODE|[0044] Detailed Description|[0045] A preparation method of blade material silicon carbide for photovoltaic wire cutting comprises the following steps:|[0046] crushing raw materials, selecting green silicon carbide block materials with the purity of more than or equal to 98 percent, carrying out jaw crushing and sieving, and collecting silicon carbide granularity sand with the granularity of less than or equal to 3 mm;|[0047] secondly, wet ball milling and grinding, and hydraulic cyclone classification, wherein the silicon carbide sand grains obtained in the first step are subjected to wet ball milling and grinding, and the hydraulic cyclone classification is carried out to obtain silicon carbide powder slurry in a required particle size range;|[0048] thirdly, automatically removing carbon through overflow, namely introducing the silicon carbide powder slurry obtained in the second step into automatic overflow carbon removal equipment, adjusting the mass concentration of the silicon carbide powder slurry to 30-50 wt%, adding 30-50 ml of flotation oil and 50-70 ml of water glass, fully stirring for 0.5-1 hour, and then overflowing to remove free carbon;|[0049] the fourth step of magnetic separation and iron removal, namely introducing the silicon carbide powder slurry obtained in the third step into magnetic separation equipment, and controlling the flow of the slurry to be 16m3/h～20m3H, removing iron-containing impurities by magnetic separation;|[0050] step five, introducing the silicon carbide powder slurry obtained in the step four into a reaction tank, adding NaOH solution according to 10-25 wt% of the mass of the slurry, controlling the temperature of the reaction tank to be 40-50 ℃, and removing free silicon and silicon dioxide after fully reacting for 2-3 hours;|[0051] sixthly, cleaning the surfaces of the particles, namely pulping, stirring and cleaning the dehydrated raw materials by adopting pure water with the conductivity of less than or equal to 10 mu s/cm for further removing metal ion impurities on the surfaces of the particles;|[0052] seventhly, overflow classification, namely introducing the cleaned slurry into an automatic overflow classification device, setting a classification program and adjusting the concentration of the slurry according to different particle size classification requirements, and performing hydraulic overflow classification, wherein water for classification is pure water with the conductivity of less than or equal to 10 mu s/cm;|[0053] step eight, centrifugal dehydration, namely performing centrifugal dehydration treatment on the slurry obtained in the step seven to ensure that the water content of the obtained powder is less than or equal to 10%;|[0054] ninth step, drying the centrifugally dewatered powder to make the water content less than 0.05%;|[0055] tenth step, mixing, namely feeding the dried powder with the same granularity section in different batches into a dry mixer for dry mixing for 1-2 hours;|[0056] and step eleven, fine screening, namely fine screening the powder obtained in the step ten by using an ultrasonic vibration screen, and removing agglomerates and large-particle impurities to obtain the silicon wafer cutting edge material.|[0057] The wet ball milling in the second step is performed by using a vertical frequency conversion wet ball mill, as shown in fig. 2, the vertical frequency conversion wet ball mill comprises a vertical ball mill barrel 5 and a stirring rod 3 installed in the barrel in a matching manner, the stirring rod 3 is driven by a variable speed motor 1 through a rotating shaft 4, a feeding hole 6 is formed in the lower part of the barrel 5 along the tangential direction, a discharging hole 2 is formed in the upper part of the barrel, and the discharging hole is connected with a feeding hole of a hydrocyclone through a water pump; the middle upper part of the hydraulic cyclone is provided with a feed inlet, the upper part of the hydraulic cyclone is provided with a rotational flow discharge port, the lower part of the hydraulic cyclone is provided with a coarse material collecting port, and the feed inlet of the middle upper part is connected with a slurry tank for collecting the discharge of the vertical frequency conversion wet ball mill through a water pump.|[0058] The vertical frequency conversion wet ball mill is formed by modifying a traditional vertical frequency conversion wet ball mill, namely, a conical buffer transition section 7 is arranged at the upper part of a vertical ball mill cylinder 5, so that large-particle micro powder which does not reach the grinding requirement can return to a grinding area in the cylinder, and a discharge pipe is arranged at the top end of the conical buffer area; the lower part of the vertical ball-milling cylinder body 5 is additionally provided with the feed inlet 6 along the tangent line, so that rotational flow is generated along the cylinder wall during feeding, large particles are brought to the milling area, and the small particles overflow the discharge port 2 along with the rotational flow. The rotation speed can be adjusted according to the crushing condition by adopting the variable frequency ball milling so as to improve the grinding efficiency; the lower part of the vertical ball mill cylinder is provided with a water inlet pipeline, so that micro powder meeting the requirement of granularity can be separated from the grinding system in time by adjusting the water inlet amount; the buffering slope that 7 buffer transition sections of the obround shape formed can make the large granule miropowder that does not reach the grinding requirement return further crushing in the barrel 5 interior grinding zone, has avoided the too much condition of large granule to appear in the product.|[0059] As shown in fig. 3, a feed inlet 2 is arranged at the middle upper part of the hydrocyclone classifier connected with a discharge outlet 6 of the vertical frequency conversion wet ball mill and connected with a water pump, ground slurry is injected into the cyclone along the tangent line of the cylinder wall of the cyclone, so that the slurry forms a cyclone in the cyclone, fine particles meeting the set particle size requirement overflow from the discharge outlet of the upper cyclone, and coarse particles not meeting the particle size requirement return to a grinding raw material collecting tank from a coarse material collecting port at the lower part for further grinding. The water flow of the feeding hole of the cyclone is adjusted by the water pump and the flow controller, and the preset classification range of the cyclone can be controlled by the caliber of the cylinder body of the discharging hole, so that the silicon carbide micro powder meeting the granularity requirement is sorted. The grinding and grading integrated device can separate slurry meeting the requirement of granularity in time and enter the next procedure. The following advantages may be achieved: firstly, the lower part of the ball mill is fed by rotational flow, slurry is prevented from sinking to the bottom, the grinding efficiency is improved, and fine particles overflow along with the rotational flow, so that over-grinding is avoided; secondly, a conical buffer transition section is adopted, coarse and fine particles are easy to classify, and overflow of large particles is reduced; and thirdly, the hydrocyclone is adopted, grinding and classification circulation are automatically carried out, and over-crushing is avoided. When the wet frequency conversion ball mill and the cyclone classifier are used for grinding and classifying, the medium balls are added according to the weight ratio of the medium balls to the silicon carbide of 2-3.5: 1, the rotating speed of a grinding head of the vertical frequency conversion wet ball mill is 100-300 rpm, and the water inflow rate of the hydraulic cyclone classifier is 100L/h-500L/h. The water inflow of the feed inlet of the ball mill is controlled, so that the micro powder meeting the requirement of granularity can be separated out in time, the undesirable conditions that the micro powder is excessively ground and the edges and corners of the micro powder are ground flat are avoided or reduced, and the production efficiency and the product quality can be improved through the adjustment of the frequency converter of the ball mill. The step is one-time grading, and the concentration of the slurry can be controlled to be 20-50% according to production requirements.|[0060] The hydrocyclone is provided with a fine material discharge port 1, a feed port 2, a discharge port and a cylinder connecting valve 3 at the middle upper part according to the figure 3, the feed port 2 is connected with a slurry tank for collecting the discharge of the wet-process variable frequency ball mill through a water pump, the middle part is a cylinder 4, the lower part is provided with a coarse material collecting port 6, and a conical buffer transition section 5 is arranged between the cylinder 4 and the coarse material collecting port 6.|[0061] And (3) during the decarbonization in the third step, when the decarbonization is carried out in automatic decarbonization equipment, adjusting the concentration of the slurry to be 50%, adding 40ml of flotation oil and 60ml of water glass, fully stirring for reaction for 1 hour, and overflowing to remove free carbon. The device is shown according to figure 4, comprising an overflow barrel 1 vertically arranged, an air inlet valve 2 is arranged at the lower end of the overflow barrel 1, the upper end of the overflow barrel 1 is connected with a diaphragm pump 3 through a pipeline, an outer overflow groove 4 and an inner overflow groove 5 are also arranged on an end cover 11 at the upper end of the overflow barrel 1, the outer overflow groove 4 is arranged at the outer side of the wall of the overflow barrel, a water inlet pipe 6 and a water outlet pipe 7 are also connected to the wall of the overflow barrel, the inner overflow groove 5 is arranged at the middle part in the overflow barrel 1, a connecting pipeline 8 is arranged between the outer overflow groove 4 and the inner overflow groove 5, the connecting pipeline 8 is also connected with a carbon collecting pool 9, and a connecting rod 10 is arranged between the end cover.|[0062] When in the fourth step of iron removal, the slurry after carbon removal is introduced and iron removal is carried out in high-gradient magnetic separation equipment, the concentration of the slurry is controlled to be 50%, and the flow is controlled to be 16m3/h。|[0063] And introducing the slurry subjected to iron removal in the alkaline washing in the fifth step, controlling the concentration of NaOH to be 20% of the whole slurry, controlling the temperature of the reaction tank to be 45 ℃, and fully reacting for 3 hours to remove free silicon and silicon dioxide.|[0064] And in the sixth step, the particle surface is cleaned by adopting pure water with the conductivity of less than 10 mu s/cm to clean the slurry after reaction, so that impurities such as metal ions and the like on the particle surface are further removed.|[0065] When the seventh step of overflow classification is carried out in an automatic control overflow classification system, the mass concentration of the slurry is controlled to be 20%, according to the setting of a program in the automatic control system, the inflow rate of water is changed between 500L/h and 1200L/h according to the overflow granularity, and 1500-mesh, 1200-mesh and 1000-mesh slurry can be obtained.|[0066] When the eighth step of dehydration is carried out in a centrifuge, the centrifugal speed is adjusted to 1200rpm, and the water content of the obtained powder is less than or equal to 10 percent.|[0067] When drying is carried out in a flash evaporation machine after the ninth step of dehydration, the temperature of hot air is controlled to be 200 ℃, and the revolution of the dispersing fan blades is 100 rpm; the number of revolutions of the classifying impeller in the classifying cylinder is 700 rpm. The flash evaporator comprises a drying cylinder, a grading cylinder and a fine powder collecting device. The drying cylinder is provided with a hot air inlet and internal dispersing fan blades, and the dispersing fan blades are controlled by a variable speed motor; the grading cylinder comprises a feeding hole, a grading impeller and a discharging hole, the feeding hole is connected with the drying cylinder, and the grading impeller is controlled by a variable speed motor; the fine powder collecting device comprises an air inducing port and a cloth bag collector.|[0068] And in the tenth step, the dried powder with the same granularity section in different batches is sent to a dry mixer for dry mixing for 2 hours.|[0069] And in the eleventh step, the fine screen is used for fine screening the powder obtained in the last step by using an ultrasonic vibration screen, and the semiconductor wafer cutting edge material is obtained after agglomeration and large-particle impurities are removed, wherein the energy gear of the ultrasonic vibration screen is set to be 80%, the adopted screen is 300 meshes, and the feeding amount is 1500 kg/h.|[0070] The performance indexes of the obtained silicon carbide blade material for photovoltaic linear cutting are shown in Table 2.|[0071] |[0072] The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and improvements can be made without departing from the technical principle of the invention, and these modifications and improvements should also be considered as the protection scope of the present invention. (CN102285654)|TECHNICAL FIELD|[0002] The invention relates to the field of multi-line cutting, in particular to a preparation method of blade material silicon carbide for solar photovoltaic silicon wafer line cutting.|BACKGROUND ART|[0004] With the rapid development of the solar photovoltaic industry, the demand for high quality silicon wafers is increasing day by day. The processing of silicon wafers is an important link in the manufacture of solar cell sets, and an effective silicon wafer cutting technology is a fundamental guarantee for obtaining high-quality silicon wafers. In recent years, the Multi-Wire Saw (Multi-Wire Saw) of the heterophoria has taken an absolute market lead in the field of large-size silicon wafer processing with its high yield and yield, and the mixed cutting agent-mortar used in the Multi-Wire cutting has an important role and plays a major role in the cutting process. The silicon carbide micro powder as a cutting edge material has wide application in the production field of solar silicon wafers and semiconductor wafers, and is an indispensable special cutting edge material in the production process of linear cutting of silicon wafers.|[0005] The prior art edge material for photovoltaic linear cutting in China has uneven quality, and has the defects of lower purity, uneven granularity, poor cutting efficiency and the like compared with the similar products in foreign countries. Domestic enterprises have backward production equipment and process, poor crushing effect, wide micro powder particle size distribution and lack of market competitiveness. At present, the production and processing modes of domestic silicon carbide cutting edge materials mainly comprise the following modes: the jet mill crushing production process has the advantages that the produced products are more than 90% in equivalent shape and higher in yield, but the jet mill is low in overall yield, the produced particles are round in shape and poor in sharpness, and recessive cracks exist and are not beneficial to cutting; the production process of Raymond mill grinding has high yield, but low yield, less volume of the produced product, and the like, which only accounts for about 50 percent, more particles with shapes of needle, sheet and the like, low cutting efficiency and poor cutting durability; in the prior art, the traditional wet ball mill is adopted for crushing, although product particles are large in volume and good in sharpness, the yield is low, the over-crushing is serious, and in addition, the acid consumption of the existing acid pickling iron removal process is large, the economy is poor, the pollution is large, and the trend of environmental protection is not met.|DISCLOSURE|[0006] Disclosure of Invention|[0007] The invention aims to provide a preparation method of blade material silicon carbide for silicon wafer linear cutting, which has the advantages of high automation, high yield, high environmental protection and low energy consumption, and the prepared silicon carbide micro powder has the advantages of concentrated granularity, multiple grades, good sharpness, high cleanliness, strong adaptability with cutting fluid, strong cutting capability and lower TTV of the cut wafer; the method has the advantages of high yield, high automation degree, small pollution, low energy consumption and good economic benefit, and is very suitable for the production method of the silicon wafer cutting edge material in large-scale production.|[0008] In order to solve the technical problems, the invention adopts the technical scheme that: a production method of a silicon wafer cutting edge material is characterized by comprising the following steps:|[0009] crushing raw materials, namely selecting green silicon carbide block materials with the purity of more than or equal to 98 percent to perform jaw crushing, and screening silicon carbide sand grains with the granularity of less than or equal to 3mm after crushing;|[0010] secondly, wet ball milling and grinding, and hydraulic cyclone classification, wherein the silicon carbide sand grains obtained in the first step are subjected to wet ball milling and grinding, and the hydraulic cyclone classification is carried out to obtain silicon carbide powder slurry in a required particle size range;|[0011] thirdly, automatically removing carbon through overflow, introducing the silicon carbide powder slurry obtained in the second step into automatic overflow carbon removal equipment, adjusting the mass concentration of the silicon carbide powder slurry to 30-50 wt%, adding 30-50 ml of flotation oil and 50-70 ml of water glass, fully stirring for 0.5-1 hour, and then overflowing to remove free carbon;|[0012] the fourth step of magnetic separation and iron removal, namely introducing the silicon carbide powder slurry obtained in the third step into magnetic separation equipment, and controlling the flow of the slurry to be 16m3/h～20m3H, removing iron-containing impurities by magnetic separation;|[0013] step five, introducing the silicon carbide powder slurry obtained in the step four into a reaction tank, adding NaOH solution according to 10-25 wt% of the mass of the slurry, controlling the temperature of the reaction tank to be 40-50 ℃, and removing free silicon and silicon dioxide after fully reacting for 2-3 hours;|[0014] sixthly, cleaning the surfaces of the particles, namely pulping, stirring and cleaning the dehydrated raw materials by adopting pure water with the conductivity of less than or equal to 10 mu s/cm for further removing metal ion impurities on the surfaces of the particles;|[0015] seventhly, overflow classification, namely introducing the cleaned slurry into an automatic overflow classification device, setting a classification program and adjusting the concentration of the slurry according to different particle size classification requirements, and performing hydraulic overflow classification, wherein the classification water is pure water with the conductivity of less than or equal to 10 us/cm;|[0016] step eight, centrifugal dehydration, namely performing centrifugal dehydration treatment on the slurry obtained in the step seven to ensure that the water content of the obtained powder is less than or equal to 10%;|[0017] ninth step, drying the centrifugally dewatered powder to make the water content less than 0.05%;|[0018] tenth step, mixing, namely feeding the dried powder with the same granularity section in different batches into a dry mixer for dry mixing for 1-2 hours;|[0019] and step eleven, fine screening, namely fine screening the powder obtained in the step ten by using an ultrasonic vibration screen, and removing agglomerates and large-particle impurities to obtain the silicon wafer cutting edge material.|[0020] The wet ball milling in the second step is carried out by selecting a vertical frequency conversion wet ball mill, the vertical frequency conversion wet ball mill comprises a vertical ball mill cylinder and a stirring rod arranged in the cylinder in a matching way, the stirring rod is driven by a variable speed motor, a feeding hole is arranged at the lower part of the cylinder along the tangential direction, a discharging hole is arranged at the upper part of the cylinder, and the discharging hole is connected with the feeding hole of the hydrocyclone through a water pump; the middle upper part of the hydraulic cyclone is provided with a feed inlet, the upper part of the hydraulic cyclone is provided with a rotational flow discharge port, the lower part of the hydraulic cyclone is provided with a coarse material collecting port, and the feed inlet of the middle upper part is connected with a slurry tank for collecting the discharge of the vertical frequency conversion wet ball mill through a water pump.|[0021] When the vertical frequency conversion wet ball mill and the hydrocyclone are used for grinding and grading, the medium balls are added according to the weight ratio of the medium balls to the silicon carbide granularity sand of 2-3.5: 1, the rotating speed of a ball grinding head of the vertical frequency conversion wet ball mill is 100-300 rpm, and the water inflow rate of the hydrocyclone is 100L/h-500L/h.|[0022] The automatic carbon removing equipment in the third step comprises an overflow barrel which is vertically arranged, an air inlet valve is arranged at the lower end of the overflow barrel, the upper end of the overflow barrel is connected with a diaphragm pump through a pipeline, an outer overflow groove and an inner overflow groove are further arranged at the upper end of the overflow barrel, the outer overflow groove is arranged on the outer side of the wall of the overflow barrel, a water inlet pipe and a water outlet pipe are further connected to the wall of the overflow barrel, the inner overflow groove is arranged in the middle of the overflow barrel, a connecting pipeline is arranged between the outer overflow groove and the inner overflow groove, and the connecting pipeline is further connected with a carbon collecting pool.|[0023] The magnetic separation equipment in the fourth step comprises a magnetic separator body and a PLC control unit, wherein a discharge hole and an air inlet for cleaning are formed in the upper portion of the magnetic separator body, and a feed inlet, a middling discharge hole and a magnetic material discharge hole are formed in the lower portion of the magnetic separator body.|[0024] The reagent used in said fifth step is aqueous NaOH solution.|[0025] In the sixth step 6, the dehydrated material is repeatedly washed 3 times or more with pure water having a conductivity of less than 10 μ s/cm to make Fe in the slurry2O3The mass percentage is less than 0.10 percent, and the total content of other heavy metals is less than 0.005 percent.|[0026] The automatic control overflow grading device in the seventh step comprises an overflow cylinder, a PLC control unit, an electric control valve and a flow sensor; and during overflow classification, controlling the inflow rate to be 500-1200L/h according to the overflow granularity, and enabling the mass concentration of the slurry to reach 15-25 wt% to obtain the slurry with the centralized granularity range.|[0027] In the eighth step, a centrifuge is adopted for concentration and dehydration, 500-2500-mesh filter cloth is adopted, and the rotation speed of the centrifuge is 800-2500 rpm; in the tenth step, the energy gear of the ultrasonic vibration sieve is adjusted to be 50-80%, and the used sieve is 200-500 meshes.|[0028] In the ninth step, the drying is carried out by adopting a flash evaporation machine; the flash evaporator comprises a drying cylinder, a grading cylinder and a fine powder collecting device; the drying cylinder is provided with a hot air inlet and internal dispersing fan blades, and the dispersing fan blades are controlled by a variable speed motor; the grading cylinder comprises a feeding hole, a grading impeller and a discharging hole, the feeding hole is connected with the drying cylinder, and the grading impeller is controlled by a variable speed motor; the fine powder collecting device comprises an air inducing port and a cloth bag collector; the hot air temperature of the air inlet of the drying cylinder is controlled to be 200-300 ℃, and the revolution of the dispersing fan blades is 100-500 rpm; the revolution of the classification impeller in the classification cylinder is 500-1500 rpm.|[0029] The invention has the positive and beneficial effects that:|[0030] 1. the silicon carbide blade material prepared by the invention is in an equal volume shape, and keeps a sharp edge angle (see figure 1), so that the balanced self-sharpening property of silicon carbide micro powder as a cutting blade material is ensured, the cutting capability is strong, the TTV of a cut silicon wafer is minimized, and the silicon carbide blade material has the characteristics of high hardness, strong wear resistance, good high-temperature resistance, high thermal conductivity and the like, and the performance indexes of the silicon carbide blade material are shown in table 1;|[0031] 2. the product particles have large specific surface area and clean appearance, and have strong adaptability with common cutting fluids such as polyethylene glycol and the like;|[0032] 3. pure water with the conductivity less than 10 mu s/cm is adopted to repeatedly elute the dehydrated material, so that the content of metal impurities in slurry is extremely low, the influence of the metal impurities on the wafer during the cutting of the semiconductor wafer is reduced, and the method plays an important role in improving the quality of the wafer;|[0033] 4. an overflow automatic carbon removal system is adopted, so that the yield is greatly improved, and the labor cost is reduced;|[0034] 5. an acid-free automatic iron removal system is adopted, so that the production cost of acid is greatly reduced, the emission pollution is reduced, and the concept of energy conservation and environmental protection is met;|[0035] 6. the product crushed by adopting the automatic system combining the wet ball mill and the hydrocyclone has the advantages of more equal volume, good sharpness and the like, and the defects of low yield, serious over-crushing and the like are avoided; the yield of the preparation method reaches more than 80 percent, the particle size distribution of the product ground by adopting the process is more uniform, the better wafer cutting effect can be achieved, and the yield (the granularity section suitable for cutting the wafer) of the common grinding process adopted in the industry is about 50 percent.|DRAWINGS DESCRIPTION|[0037] FIG. 1 is a scanning electron micrograph of a silicon wafer cutting edge material produced by the method of the present invention;|[0038] FIG. 2 is a schematic diagram of the structure of a wet ball mill modified in the method of the present invention;|[0039] FIG. 3 is a schematic diagram of the construction of a hydrocyclone used in the process of the present invention;|[0040] FIG. 4 is a schematic structural view of an automatic carbon removal apparatus used in the method of the present invention.|[0041] In fig. 2: 1. a variable speed motor; 2. a discharge port; 3. a stirring rod; 4. a rotating shaft; 5. a barrel; 6. a feed inlet; 7. a conical buffer transition section.|[0042] In fig. 3: 1. a fine material discharge port of the cyclone; 2. a feed inlet; 3. the discharge port is connected with the cylinder body through a valve; 4. a barrel; 5. a conical buffer transition section 6 and a coarse material discharge port.|[0043] In fig. 4: 1. an overflow bucket; 2 is an air inlet valve; 3. a diaphragm pump; 4. an overflow chute; 5. an inner overflow launder; 6. a water inlet pipe; 7. a water outlet pipe; 8. a pipeline; 9. a carbon collecting pool; 10. a connecting rod; 11. and (4) end covers.|INVENTION MODE|[0044] Detailed Description|[0045] A preparation method of blade material silicon carbide for photovoltaic wire cutting comprises the following steps:|[0046] crushing raw materials, selecting green silicon carbide block materials with the purity of more than or equal to 98 percent, carrying out jaw crushing and sieving, and collecting silicon carbide granularity sand with the granularity of less than or equal to 3 mm;|[0047] secondly, wet ball milling and grinding, and hydraulic cyclone classification, wherein the silicon carbide sand grains obtained in the first step are subjected to wet ball milling and grinding, and the hydraulic cyclone classification is carried out to obtain silicon carbide powder slurry in a required particle size range;|[0048] thirdly, automatically removing carbon through overflow, namely introducing the silicon carbide powder slurry obtained in the second step into automatic overflow carbon removal equipment, adjusting the mass concentration of the silicon carbide powder slurry to 30-50 wt%, adding 30-50 ml of flotation oil and 50-70 ml of water glass, fully stirring for 0.5-1 hour, and then overflowing to remove free carbon;|[0049] the fourth step of magnetic separation and iron removal, namely introducing the silicon carbide powder slurry obtained in the third step into magnetic separation equipment, and controlling the flow of the slurry to be 16m3/h～20m3H, removing iron-containing impurities by magnetic separation;|[0050] step five, introducing the silicon carbide powder slurry obtained in the step four into a reaction tank, adding NaOH solution according to 10-25 wt% of the mass of the slurry, controlling the temperature of the reaction tank to be 40-50 ℃, and removing free silicon and silicon dioxide after fully reacting for 2-3 hours;|[0051] sixthly, cleaning the surfaces of the particles, namely pulping, stirring and cleaning the dehydrated raw materials by adopting pure water with the conductivity of less than or equal to 10 mu s/cm for further removing metal ion impurities on the surfaces of the particles;|[0052] seventhly, overflow classification, namely introducing the cleaned slurry into an automatic overflow classification device, setting a classification program and adjusting the concentration of the slurry according to different particle size classification requirements, and performing hydraulic overflow classification, wherein water for classification is pure water with the conductivity of less than or equal to 10 mu s/cm;|[0053] step eight, centrifugal dehydration, namely performing centrifugal dehydration treatment on the slurry obtained in the step seven to ensure that the water content of the obtained powder is less than or equal to 10%;|[0054] ninth step, drying the centrifugally dewatered powder to make the water content less than 0.05%;|[0055] tenth step, mixing, namely feeding the dried powder with the same granularity section in different batches into a dry mixer for dry mixing for 1-2 hours;|[0056] and step eleven, fine screening, namely fine screening the powder obtained in the step ten by using an ultrasonic vibration screen, and removing agglomerates and large-particle impurities to obtain the silicon wafer cutting edge material.|[0057] The wet ball milling in the second step is performed by using a vertical frequency conversion wet ball mill, as shown in fig. 2, the vertical frequency conversion wet ball mill comprises a vertical ball mill barrel 5 and a stirring rod 3 installed in the barrel in a matching manner, the stirring rod 3 is driven by a variable speed motor 1 through a rotating shaft 4, a feeding hole 6 is formed in the lower part of the barrel 5 along the tangential direction, a discharging hole 2 is formed in the upper part of the barrel, and the discharging hole is connected with a feeding hole of a hydrocyclone through a water pump; the middle upper part of the hydraulic cyclone is provided with a feed inlet, the upper part of the hydraulic cyclone is provided with a rotational flow discharge port, the lower part of the hydraulic cyclone is provided with a coarse material collecting port, and the feed inlet of the middle upper part is connected with a slurry tank for collecting the discharge of the vertical frequency conversion wet ball mill through a water pump.|[0058] The vertical frequency conversion wet ball mill is formed by modifying a traditional vertical frequency conversion wet ball mill, namely, a conical buffer transition section 7 is arranged at the upper part of a vertical ball mill cylinder 5, so that large-particle micro powder which does not reach the grinding requirement can return to a grinding area in the cylinder, and a discharge pipe is arranged at the top end of the conical buffer area; the lower part of the vertical ball-milling cylinder body 5 is additionally provided with the feed inlet 6 along the tangent line, so that rotational flow is generated along the cylinder wall during feeding, large particles are brought to the milling area, and the small particles overflow the discharge port 2 along with the rotational flow. The rotation speed can be adjusted according to the crushing condition by adopting the variable frequency ball milling so as to improve the grinding efficiency; the lower part of the vertical ball mill cylinder is provided with a water inlet pipeline, so that micro powder meeting the requirement of granularity can be separated from the grinding system in time by adjusting the water inlet amount; the buffering slope that 7 buffer transition sections of the obround shape formed can make the large granule miropowder that does not reach the grinding requirement return further crushing in the barrel 5 interior grinding zone, has avoided the too much condition of large granule to appear in the product.|[0059] As shown in fig. 3, a feed inlet 2 is arranged at the middle upper part of the hydrocyclone classifier connected with a discharge outlet 6 of the vertical frequency conversion wet ball mill and connected with a water pump, ground slurry is injected into the cyclone along the tangent line of the cylinder wall of the cyclone, so that the slurry forms a cyclone in the cyclone, fine particles meeting the set particle size requirement overflow from the discharge outlet of the upper cyclone, and coarse particles not meeting the particle size requirement return to a grinding raw material collecting tank from a coarse material collecting port at the lower part for further grinding. The water flow of the feeding hole of the cyclone is adjusted by the water pump and the flow controller, and the preset classification range of the cyclone can be controlled by the caliber of the cylinder body of the discharging hole, so that the silicon carbide micro powder meeting the granularity requirement is sorted. The grinding and grading integrated device can separate slurry meeting the requirement of granularity in time and enter the next procedure. The following advantages may be achieved: firstly, the lower part of the ball mill is fed by rotational flow, slurry is prevented from sinking to the bottom, the grinding efficiency is improved, and fine particles overflow along with the rotational flow, so that over-grinding is avoided; secondly, a conical buffer transition section is adopted, coarse and fine particles are easy to classify, and overflow of large particles is reduced; and thirdly, the hydrocyclone is adopted, grinding and classification circulation are automatically carried out, and over-crushing is avoided. When the wet frequency conversion ball mill and the cyclone classifier are used for grinding and classifying, the medium balls are added according to the weight ratio of the medium balls to the silicon carbide of 2-3.5: 1, the rotating speed of a grinding head of the vertical frequency conversion wet ball mill is 100-300 rpm, and the water inflow rate of the hydraulic cyclone classifier is 100L/h-500L/h. The water inflow of the feed inlet of the ball mill is controlled, so that the micro powder meeting the requirement of granularity can be separated out in time, the undesirable conditions that the micro powder is excessively ground and the edges and corners of the micro powder are ground flat are avoided or reduced, and the production efficiency and the product quality can be improved through the adjustment of the frequency converter of the ball mill. The step is one-time grading, and the concentration of the slurry can be controlled to be 20-50% according to production requirements.|[0060] The hydrocyclone is provided with a fine material discharge port 1, a feed port 2, a discharge port and a cylinder connecting valve 3 at the middle upper part according to the figure 3, the feed port 2 is connected with a slurry tank for collecting the discharge of the wet-process variable frequency ball mill through a water pump, the middle part is a cylinder 4, the lower part is provided with a coarse material collecting port 6, and a conical buffer transition section 5 is arranged between the cylinder 4 and the coarse material collecting port 6.|[0061] And (3) during the decarbonization in the third step, when the decarbonization is carried out in automatic decarbonization equipment, adjusting the concentration of the slurry to be 50%, adding 40ml of flotation oil and 60ml of water glass, fully stirring for reaction for 1 hour, and overflowing to remove free carbon. The device is shown according to figure 4, comprising an overflow barrel 1 vertically arranged, an air inlet valve 2 is arranged at the lower end of the overflow barrel 1, the upper end of the overflow barrel 1 is connected with a diaphragm pump 3 through a pipeline, an outer overflow groove 4 and an inner overflow groove 5 are also arranged on an end cover 11 at the upper end of the overflow barrel 1, the outer overflow groove 4 is arranged at the outer side of the wall of the overflow barrel, a water inlet pipe 6 and a water outlet pipe 7 are also connected to the wall of the overflow barrel, the inner overflow groove 5 is arranged at the middle part in the overflow barrel 1, a connecting pipeline 8 is arranged between the outer overflow groove 4 and the inner overflow groove 5, the connecting pipeline 8 is also connected with a carbon collecting pool 9, and a connecting rod 10 is arranged between the end cover.|[0062] When in the fourth step of iron removal, the slurry after carbon removal is introduced and iron removal is carried out in high-gradient magnetic separation equipment, the concentration of the slurry is controlled to be 50%, and the flow is controlled to be 16m3/h。|[0063] And introducing the slurry subjected to iron removal in the alkaline washing in the fifth step, controlling the concentration of NaOH to be 20% of the whole slurry, controlling the temperature of the reaction tank to be 45 ℃, and fully reacting for 3 hours to remove free silicon and silicon dioxide.|[0064] And in the sixth step, the particle surface is cleaned by adopting pure water with the conductivity of less than 10 mu s/cm to clean the slurry after reaction, so that impurities such as metal ions and the like on the particle surface are further removed.|[0065] When the seventh step of overflow classification is carried out in an automatic control overflow classification system, the mass concentration of the slurry is controlled to be 20%, according to the setting of a program in the automatic control system, the inflow rate of water is changed between 500L/h and 1200L/h according to the overflow granularity, and 1500-mesh, 1200-mesh and 1000-mesh slurry can be obtained.|[0066] When the eighth step of dehydration is carried out in a centrifuge, the centrifugal speed is adjusted to 1200rpm, and the water content of the obtained powder is less than or equal to 10 percent.|[0067] When drying is carried out in a flash evaporation machine after the ninth step of dehydration, the temperature of hot air is controlled to be 200 ℃, and the revolution of the dispersing fan blades is 100 rpm; the number of revolutions of the classifying impeller in the classifying cylinder is 700 rpm. The flash evaporator comprises a drying cylinder, a grading cylinder and a fine powder collecting device. The drying cylinder is provided with a hot air inlet and internal dispersing fan blades, and the dispersing fan blades are controlled by a variable speed motor; the grading cylinder comprises a feeding hole, a grading impeller and a discharging hole, the feeding hole is connected with the drying cylinder, and the grading impeller is controlled by a variable speed motor; the fine powder collecting device comprises an air inducing port and a cloth bag collector.|[0068] And in the tenth step, the dried powder with the same granularity section in different batches is sent to a dry mixer for dry mixing for 2 hours.|[0069] And in the eleventh step, the fine screen is used for fine screening the powder obtained in the last step by using an ultrasonic vibration screen, and the semiconductor wafer cutting edge material is obtained after agglomeration and large-particle impurities are removed, wherein the energy gear of the ultrasonic vibration screen is set to be 80%, the adopted screen is 300 meshes, and the feeding amount is 1500 kg/h.|[0070] The performance indexes of the obtained silicon carbide blade material for photovoltaic linear cutting are shown in Table 2.|[0071] |[0072] The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and improvements can be made without departing from the technical principle of the invention, and these modifications and improvements should also be considered as the protection scope of the present invention. Family Number|(7517240)|7517240|Abstract|(CN102285654B B)|The invention relates to a production method of a silicon wafer cutting blade material . The production method of the silicon wafer cutting blade material uses high - purity green silicon carbide as the raw material and comprises the following steps : performing jaw crushing , screening , performing automatic circulation type wet ball milling and hydraulic cyclone classification , performing automatic overflow carbon removal , performing magnetic separation to automatically remove iron , performing alkali washing , cleaning , performing overflow classification under automatic control of a programmable logic controller ( PLC ) , centrifuging to dewater , drying , mixing , performing fine screening and the like . The silicon carbide blade material prepared by the method has equiareal shape , sharp edges and high cutting capability ; the blade material particles have large specific surface area and clean appearance and high suitability to cutting fluid such as polyethylene glycol ; the product ground by automatic circulation type wet ball milling and cyclone classification has more equiareal shapes , good grain shape and high yield , and overgrinding can be avoided ; and automatic magnetic separation is adopted to perform acid - free iron removal , thus the method has high efficiency , environmental friendliness and high degree of automation and is suitable for large - scale production . The product ground by the method has high particle size concentration degree and good grain shape , and better cutting effect can be realized . |IPC codes|(CN102285654B B)|C01B - 031/36 | Chemical engineering|Materials, metallurgy B02C-001/02|B02C-017/16|C01B-031/36 B02C-001/02|B02C-017/16|C01B-031/36 CN111377448|CN109107729|CN104925811|CN105668570|CN118768054|CN111672891|CN111151169|CN110370442|CN109876510|CN109092515B|CN108837926B|CN109956475|CN105597898|CN105498929|CN104211064B|US20200207630|CN115634744B|CN113546729B|US11718532|CN103922343B|CN103523783B CN111377448 89518100 WHO=Examiner SELF=N CAT=Y|CN109107729 82810257 WHO=Examiner SELF=N CAT=Y|CN104925811 70935290 WHO=Examiner SELF=N CAT=Y|CN105668570 73317340 WHO=Examiner SELF=N CAT=X|CN118768054 111776146 WHO=Examiner SELF=N CAT=A|CN111672891 90688237 WHO=Examiner SELF=N CAT=A|CN111151169 88796779 WHO=Examiner SELF=N CAT=A|CN110370442 86414633 WHO=Examiner SELF=N CAT=A|CN109876510 84853785 WHO=Examiner SELF=N CAT=A|CN109092515B 82771464 WHO=Examiner SELF=N CAT=A|CN108837926B 82052923 WHO=Examiner SELF=N CAT=A|CN109956475 85048471 WHO=Examiner SELF=N CAT=A|CN105597898 73114727 WHO=Examiner SELF=N CAT=A|CN105498929 72703511 WHO=Examiner SELF=N CAT=A|CN104211064B 68159535 WHO=Examiner SELF=N CAT=A|US20200207630 89518100 WHO=Examiner SELF=N CAT=103|CN115634744B 103592119 WHO=Examiner SELF=N|CN113546729B 96634721 WHO=Examiner SELF=N|US11718532 89518100 WHO=Applicant SELF=N|CN103922343B 66693682 WHO=Examiner SELF=N|CN103523783B 59568053 WHO=Examiner SELF=N CN101891194|CN101947483|US20100032630|CN1911798 CN101891194 7129613 WHO=Examiner SELF=N CAT=X|CN101947483 7173439 WHO=Examiner SELF=N CAT=A|US20100032630 44255217 WHO=Examiner SELF=N CAT=A|CN1911798 5320126 WHO=Examiner SELF=N CAT=A CN101891194; CN101947483; CN1911798; US20100032630 LAPSED (CN102285654)|LAPSED DEAD (CN102285654)|DEAD (CN102285654)|LEGAL DETAILS FOR CN102285654|Actual or expected expiration date=2018-06-02|Legal state=DEAD|Status=LAPSED|Event publication date=2011-06-02|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201110146445|Application date=2011-06-02|Standardized application number=2011CN-0146445|Event publication date=2011-12-21|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN102285654|Publication stage code=A|Publication date=2011-12-21|Standardized publication number=CN102285654|Event publication date=2011-12-21|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2012-02-08|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2013-09-04|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN102285654|Publication stage code=B|Publication date=2013-09-04|Standardized publication number=CN102285654B|Event publication date=2013-09-04|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2019-05-28|Event code=CN/CF01|Event indicator=Neg|Event group=Event indicating Not In Force|Termination of patent right due to non-payment of annual fee|Effective date of the event=2018-06-02 https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjlRxiSVqgNQjhj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000001126982&ekey=2261&xpn=CN102285654B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=EekTDBO26R3WfDGX1p4lpbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN102285654)|NAME=WANG PENG|NAME=LI HONG|NAME=WANG YI|(CN102285654)|NAME=WANG PENG|NAME=LI HONG|NAME=WANG YI 0 1 Titre: (CN102285654)|Production method of silicon wafer cutting blade material Résumé: (CN102285654)|The invention relates to a production method of a silicon wafer cutting blade material. The production method of the silicon wafer cutting blade material uses high-purity green silicon carbide as the raw material and comprises the following steps: performing jaw crushing, screening, performing automatic circulation type wet ball milling and hydraulic cyclone classification, performing automatic overflow carbon removal, performing magnetic separation to automatically remove iron, performing alkali washing, cleaning, performing overflow classification under automatic control of a programmable logic controller (PLC), centrifuging to dewater, drying, mixing, performing fine screening and the like. The silicon carbide blade material prepared by the method has equiareal shape, sharp edges and high cutting capability; the blade material particles have large specific surface area and clean appearance and high suitability to cutting fluid such as polyethylene glycol; the product ground by automatic circulation type wet ball milling and cyclone classification has more equiareal shapes, good grain shape and high yield, and overgrinding can be avoided; and automatic magnetic separation is adopted to perform acid-free iron removal, thus the method has high efficiency, environmental friendliness and high degree of automation and is suitable for large-scale production. The product ground by the method has high particle size concentration degree and good grain shape, and better cutting effect can be realized. 99 Abstract gpt-4o-mini no The article focuses on the production method of silicon wafer cutting blade material and does not relate to accelerated weathering or CO₂ capture.
101 CN202111367677|WOCN2022/011181|WOCN2022/111816 WOCN2022/111816|ES202390075|DE112022000199|MX2023014158|US18/260,005|GB202313003|WOCN2022/011181|HUP2300206|CN202111367677 ES2963369|DE112022000199|HU231541|MX415021|US12009492|GB2620690|ES2963369|MX2023014158|US20240063451|GB2620690|GB2620690|GB202313003|HUP2300206|DE112022000199|WO2023/087800|CN114229816|CN114229816 99304691 WO2023/087800 A1 2023-05-25 [WO202387800]|ES2963369 R1 2026-01-15 [ES2963369]|ES2963369 A2 2024-03-26 [ES2963369]|DE112022000199 B4 2024-11-21 [DE112022000199]|DE112022000199 T5 2023-08-10 [DE112022000199]|MX415021 B 2024-07-17 [MX-415021]|MX2023014158 A 2024-02-29 [MX2023014158]|US12009492 B2 2024-06-11 [US12009492]|US20240063451 A1 2024-02-22 [US20240063451]|GB2620690 B 2024-06-05 [GB2620690]|GB2620690 A8 2024-02-21 [GB2620690]|GB2620690 A 2024-01-17 [GB2620690]|GB202313003 D0 2023-10-11 [GB202313003]|HU231541 B1 2024-09-28 [HU-231541]|HUP2300206 A2 2023-09-28 [HUP2300206]|CN114229816 B 2023-04-11 [CN114229816B]|CN114229816 A 2022-03-25 [CN114229816] 2021-11-18|2022-08-11 2022-08-11|2022-08-11|2022-08-11|2022-08-11|2022-08-11|2022-08-11|2022-08-11|2022-08-11|2021-11-18 2026-01-15|2024-11-21|2024-09-28|2024-07-17|2024-06-11|2024-06-05|2024-03-26|2024-02-29|2024-02-22|2024-02-21|2024-01-17|2023-10-11|2023-09-28|2023-08-10|2023-05-25|2023-04-11|2022-03-25 (US12009492)|2024-06-11||(GB2620690)|2024-06-05|(DE112022000199)|2024-11-21|(CN114229816B)|2023-04-11|(HU-231541)|2024-09-28|(MX-415021)|2024-07-17| (US12009492)|2042-08-11|(WO2023/087800)|2025-05-18|(GB2620690)|2042-08-11|(DE112022000199)|2042-08-11|(CN114229816)|2041-11-18|(HU231541)|2042-08-11|(MX415021)|2042-08-11|(ES2963369)|2042-08-11 (US12009492)|Method for recycling and preparing positive electrode material from waste lithium iron phosphate batteries (US12009492)|A method for recycling and preparing a positive electrode material from waste lithium iron phosphate batteries. The method comprises the following steps: discharging, crushing, and stripping waste lithium iron phosphate batteries to obtain black powder; then mixing the black powder with benzenesulfonate, and reacting in a fluidized bed; and then adding an acid and an alkali to remove impurities, finally adding a lithium supplement, an iron supplement, or a phosphate, and a reducing agent, and sintering. According to the method, by controlling and optimizing the crushing, stripping, carbon and fluorine removal, and impurity removal processes, a positive electrode material with high purity can be recycled while controlling the recycling cost, and batteries prepared by means of the recycled positive electrode material have good performance. GUANGDONG BRUNP RECYCLING TECHNOLOGY|HUNAN BRUNP RECYCLING TECHNOLOGY|YICHANG BRUNP CONTEMPORARY AMPEREX (US12009492)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. ([CN])|HUNAN BRUNP RECYCLING TECHNOLOGY CO., LTD ([CN])|YICHANG BRUNP CONTEMPORARY AMPEREX CO., LTD. ([CN])|(US20240063451)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. ([CN])|HUNAN BRUNP RECYCLING TECHNOLOGY CO., LTD. ([CN])|YICHANG BRUNP CONTEMPORARY AMPEREX CO., LTD. ([CN])|(WO2023/087800)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. ([CN])|HUNAN BRUNP RECYCLING TECHNOLOGY CO., LTD. ([CN])|YICHANG BRUNP CONTEMPORARY AMPEREX CO., LTD. ([CN])|(GB2620690)|Guangdong Brunp Recycling Technology Co., Ltd.|Hunan Brunp Recycling Technology Co., Ltd.|Yichang Brunp Contemporary Amperex Co., Ltd.|(GB2620690)|Guangdong Brunp Recycling Technology Co., Ltd.|Hunan Brunp Recycling Technology Co., Ltd.|Yichang Brunp Contemporary Amperex Co., Ltd.|(GB2620690)|Guangdong Brunp Recycling Technology Co., Ltd.|Hunan Brunp Recycling Technology Co., Ltd.|Yichang Brunp Recycling Technology Co. Ltd.|(GB202313003)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO LTD|HUNAN BRUNP RECYCLING TECH CO LTD|YICHANG BRUNP RECYCLING TECH CO LTD|(DE112022000199)|Guangdong Brunp Recycling Technology Co., Ltd. ([CN])|Hunan Brunp Recycling Technology Co., Ltd. ([CN])|Yichang Brunp Contemporary Amperex Co., Ltd. ([CN])|(DE112022000199)|Guangdong Brunp Recycling Technology Co., Ltd. ([CN])|Hunan Brunp Recycling Technology Co., Ltd. ([CN])|Yichang Brunp Contemporary Amperex Co., Ltd. ([CN])|(CN114229816)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. ([CN])|HUNAN BRUNP RECYCLING TECHNOLOGY CO. LTD.|YICHANG BRUNP CONTEMPORARY AMPEREX CO., LTD.|(CN114229816)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. ([CN])|HUNAN BRUNP RECYCLING TECHNOLOGY CO. LTD.|YICHANG BRUNP CONTEMPORARY AMPEREX CO., LTD.|(HU231541)|Guangdong Brunp Recycling Technology Co|Hunan Brunp Recycling Technology Co|Yichang Brunp Contemporary Amperex Co|(HUP2300206)|Guangdong Brunp Recycling Technology Co|Hunan Brunp Recycling Technology Co|Yichang Brunp Contemporary Amperex Co|(MX415021)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO LTD ([CN])|(MX2023014158)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO LTD ([CN])|(ES2963369)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD.|HUNAN BRUNP RECYCLING TECHNOLOGY CO., LTD.|YICHANG BRUNP CONTEMPORARY AMPEREX CO., LTD.|(ES2963369)|GUANGDONG BRUNP RECYCLING TECHNOLOGY CO LTD ([CN])|HUNAN BRUNP RECYCLING TECH CO LTD ([CN])|YICHANG BRUNP CONTEMPORARY AMPEREX CO LTD ([CN]) YU HAIJUN|LI AIXIA|XIE YINGHAO|LI CHANGDONG|ZHANG XUEMEI|ZHONG YINGSHENG (US12009492)|Yu Haijun|Li Aixia|Xie Yinghao|Li Changdong|Zhang Xuemei|Zhong Yingsheng|(US20240063451)|YU Haijun|LI Aixia|XIE Yinghao|LI Changdong|ZHANG Xuemei|ZHONG Yingsheng (US12009492)|Buchalter|Croft Jason W.|(WO2023/087800)|JIAQUAN IP LAW ([CN])|(DE112022000199)|Spies & Behrndt Patentanwälte PartG mbB ([DE])|(CN114229816)|HUANG FEIFEI;JIAQUAN IP LAW|Reg. Nb: 44205|(MX415021)|LUISA IRELY AQUIQUE PINEDA (US12009492)|Especially, the crushing of aluminum and copper foils makes the aluminum and copper foils be mixed with each other, and the mixture cannot be separated accurately by mechanical separation.|There are still some problems in this recycling method, for example, during mechanical crushing, waste polyanion batteries may be affected by crushed shells and crushed current collectors and diaphragms, so as to change physical and chemical components of a cathode material to be recycled.| (US12009492)|1. A method for recycling and preparing a cathode material from waste lithium iron phosphate batteries, comprising: (1) discharging the waste lithium iron phosphate batteries, drying an electrolyte inside the waste lithium iron phosphate batteries, then crushing to obtain crushed pieces, and stripping the crushed pieces to obtain a black powder; (2) mixing the black powder obtained in step (1) with a benzene sulfonate, and then reacting in a fluidized bed to obtain a black powder with carbon and fluorine being removed; (3) adding an acid into the black powder with carbon and fluorine being removed in step (2), performing solid-liquid separation to obtain a solution A and a solid A; and then, adding an alkali into the solution A until no precipitation is generated, and performing solid-liquid separation to obtain a solution B and a solid B; and (4) mixing the solid A and the solution B obtained in step (3), adding at least one of a lithium supplement agent, an iron supplement agent or a phosphate to obtain a mixture, then adding a reducing agent into the mixture, and sintering to obtain the cathode material.| (US12009492)|The present disclosure aims at solving at least one of the above-mentioned technical problems in the prior art.|The present disclosure relates to the technical field of recycling battery materials, and particularly, to a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery.|This application is a national stage filing under 35 U.S.C. § 371 of international application number PCT/CN2022/111816, filed Aug. 11, 2022, which claims priority to Chinese patent application No. 202111367677.5, filed Nov. 18, 2021.| (US12009492)|LITHIUM IRON PHOSPHATE(100,57)|LITHIUM IRON PHOSPHATE BATTERY(100,41)|CATHODE(100,17)|RECYCLING(100,16)|LITHIUM SUPPLEMENT(100,3)|POSITIVE ELECTRODE(100,3)|WASTE POLYANION BATTERY(99,1)|PHOSPHO ESTER(77,9)|CRUSHED PIECE(70,26)|NATIONAL STAGE FILING(67,1)|CRUSHED SHELL(63,1)|ALUMINUM CRUSHING(62,1)|PHOSPHO MONOESTER(58,2)|PHOSPHO TRIESTER(52,2)|CRUSHING(50,6)|BLACK POWDER(43,59)|CRUSHED CURRENT COLLECTOR(36,1)|REMOVING FLUORINE(35,1)|STRIPPING LIQUID(34,22)|BENZENE SULFONATE(34,11)|COPPER FOIL(34,7)|FLUORINE(33,43)|IRON SUPPLEMENT(33,4)|BATTERY MATERIAL RECYCLING(30,1)|FLUIDIZED BED(29,11)|ELECTROLYTE(29,9)|PRECIPITATION(29,7)|DIAPHRAGM(26,3)|DISCHARGING(26,1)|RECYCLING COST(25,5)|PRIMARY HEAT(24,5)|PHOSPHODIESTER(24,2)|CATHODE CHEMICAL COMPONENT(23,1)|PRETREATING BATTERY(22,5)|ZINC BENZENESULFONATE(22,2)|POLYOL VOLUME RATIO(21,4)|PHOSPHATE RADICAL(20,6)|SODIUM BENZENESULFONATE(19,2)|TRIMETHYL PHOSPHATE(19,2)|IMPURITY REMOVAL(18,1)|RECYCLED POSITIVE ELECTRODE MATERIAL(18,1)|SOLID LIQUID SEPARATION(16,14)|TRIETHYL PHOSPHATE(16,7)|REDUCING AGENT(16,4)|DRY ELECTROLYTE(15,5)|FLUIDIZED BED PUMP(15,5)|NEON ENVIRONMENT(15,5)|REMOVING IMPURITY(15,5)|MEMBRANE PYROLYSIS(15,2)|PROPYLENE GLYCOL(15,2)|MOLAR RATIO(14,11)|CRUSHED PIECE AREA RATIO(14,8)|ETHYLENE GLYCOL(14,2)|CATHODE MATERIAL(13,20)|FERROUS OXALATE(12,6)|REGENERATED LITHIUM IRON PHOSPHATE(12,6)|SEPARATION LIQUID(11,11)|EVAPORATED SOLID(11,5)|POLYVINYLIDENE FLUORIDE(11,5)|HEATING FURNACE(11,3)|FLUORINE COMPARATIVE(11,2)|CHEMICAL COMPONENT(11,1)|FLUORINE PYROLYSIS(11,1)|FLUIDIZED BED PYROLYSIS(10,1)|SINTERING FURNACE(10,1)|MAH(9,8)|SEM GRAPH(9,2)|SODIUM P TOLUENESULFONATE(8,8)|CALCIUM HYDROXIDE(8,6)|GLUCOSE(8,6)|LITHIUM CARBONATE(8,6)|SOLAR RADIATION(8,6)|DISCHARGE CAPACITY(8,3)|HEAT PIPE(8,2)|ACETYLENE BLACK(8,1)|FERRIC HYDROXIDE(8,1)|BALL MILLING(7,5)|COMBUSTION CHAMBER(7,5)|HEATER(7,5)|HEATING TEMPERATURE(7,5)|PROPANETRIOL VOLUME RATIO(7,5)|PUMP AIR(7,5)|REGENERATING CATHODE MATERIAL(7,5)|PLATE ACTIVE SUBSTANCE(6,15)|BINDER(6,4)|LIPF(6,4)|METAL SALT(6,4)|BATTERY ASSEMBLY(6,1)|CONVEYING CAPACITY(6,1)|STRIPPING TREATMENT(6,1)|WORKING VOLTAGE PLATFORM(6,1)|LICLO(5,3)|BASE ADDITION(5,1)|BLACK POWDER FLUORINE CONTENT(5,1)|CAPACITY DENSITY(5,1)|CLEAN ALUMINUM FOIL(5,1)|ELASTIC SHEET(5,1)|FERRIC CITRATE(5,1)|FERRIC OXALATE(5,1)|FERROUS CITRATE(5,1)|FRUCTOSE(5,1)|INTERNATIONAL APPLICATION NUMBER PCT CN(5,1)|ISOPROPANOL(5,1)|LATE REMOVAL(5,1)||(US20240063451)|LITHIUM IRON PHOSPHATE(100,57)|LITHIUM IRON PHOSPHATE BATTERY(100,41)|CATHODE(100,17)|RECYCLING(100,15)|LITHIUM SUPPLEMENT(100,3)|POSITIVE ELECTRODE(100,3)|WASTE POLYANION BATTERY(99,1)|PHOSPHO ESTER(77,9)|CRUSHED PIECE(70,26)|CRUSHED SHELL(63,1)|ALUMINUM CRUSHING(62,1)|PHOSPHO MONOESTER(58,2)|PHOSPHO TRIESTER(52,2)|CRUSHING(50,6)|BLACK POWDER(43,59)|CRUSHED CURRENT COLLECTOR(36,1)|REMOVING FLUORINE(35,1)|STRIPPING LIQUID(34,22)|BENZENE SULFONATE(34,11)|COPPER FOIL(34,7)|FLUORINE(33,43)|IRON SUPPLEMENT(33,4)|BATTERY MATERIAL RECYCLING(30,1)|FLUIDIZED BED(29,11)|ELECTROLYTE(29,9)|PRECIPITATION(29,7)|DIAPHRAGM(26,3)|DISCHARGING(26,1)|RECYCLING COST(25,5)|PRIMARY HEAT(24,5)|PHOSPHODIESTER(24,2)|CATHODE CHEMICAL COMPONENT(23,1)|PRETREATING BATTERY(22,5)|ZINC BENZENESULFONATE(22,2)|POLYOL VOLUME RATIO(21,4)|ISOPROPANOL(21,2)|PHOSPHATE RADICAL(20,6)|SODIUM BENZENESULFONATE(19,2)|TRIMETHYL PHOSPHATE(19,2)|IMPURITY REMOVAL(18,1)|RECYCLED POSITIVE ELECTRODE MATERIAL(18,1)|BUTANOL(17,2)|SOLID LIQUID SEPARATION(16,14)|TRIETHYL PHOSPHATE(16,7)|REDUCING AGENT(16,4)|DRY ELECTROLYTE(15,5)|FLUIDIZED BED PUMP(15,5)|NEON ENVIRONMENT(15,5)|REMOVING IMPURITY(15,5)|MEMBRANE PYROLYSIS(15,2)|PROPYLENE GLYCOL(15,2)|MOLAR RATIO(14,11)|CRUSHED PIECE AREA RATIO(14,8)|ETHYLENE GLYCOL(14,2)|CATHODE MATERIAL(13,20)|FERROUS OXALATE(12,6)|REGENERATED LITHIUM IRON PHOSPHATE(12,6)|SEPARATION LIQUID(11,11)|EVAPORATED SOLID(11,5)|POLYVINYLIDENE FLUORIDE(11,5)|HEATING FURNACE(11,3)|FLUORINE COMPARATIVE(11,2)|CHEMICAL COMPONENT(11,1)|FLUORINE PYROLYSIS(11,1)|FLUIDIZED BED PYROLYSIS(10,1)|SINTERING FURNACE(10,1)|MAH(9,8)|SEM GRAPH(9,2)|SODIUM P TOLUENESULFONATE(8,8)|CALCIUM HYDROXIDE(8,6)|GLUCOSE(8,6)|LITHIUM CARBONATE(8,6)|SOLAR RADIATION(8,6)|DISCHARGE CAPACITY(8,3)|HEAT PIPE(8,2)|ACETYLENE BLACK(8,1)|FERRIC HYDROXIDE(8,1)|BALL MILLING(7,5)|COMBUSTION CHAMBER(7,5)|HEATER(7,5)|HEATING TEMPERATURE(7,5)|PROPANETRIOL VOLUME RATIO(7,5)|PUMP AIR(7,5)|REGENERATING CATHODE MATERIAL(7,5)|PLATE ACTIVE SUBSTANCE(6,15)|BINDER(6,4)|LIPF(6,4)|METAL SALT(6,4)|BATTERY ASSEMBLY(6,1)|CONVEYING CAPACITY(6,1)|STRIPPING TREATMENT(6,1)|WORKING VOLTAGE PLATFORM(6,1)|LICLO(5,3)|BASE ADDITION(5,1)|BLACK POWDER FLUORINE CONTENT(5,1)|CAPACITY DENSITY(5,1)|CLEAN ALUMINUM FOIL(5,1)|ELASTIC SHEET(5,1)|FERRIC CITRATE(5,1)|FERRIC OXALATE(5,1)|FERROUS CITRATE(5,1)|FRUCTOSE(5,1)|LATE REMOVAL(5,1)||(WO2023/087800)|LITHIUM IRON PHOSPHATE(100,22)|LITHIUM IRON PHOSPHATE BATTERY(100,21)|POSITIVE ELECTRODE(100,19)|SPENT LITHIUM FERRIC PHOSPHATE(100,12)|LITHIUM SUPPLEMENT(98,3)|BENZENESULFONATE SALT(97,4)|FLUORINE STRIPPED BLACK POWDER(86,4)|CASING CRUSHING(81,1)|CRUSHED PIECE(77,4)|SPENT LITHIUM(76,12)|POLYANIONIC CELL(65,1)|STRIPPED BLACK POWDER(62,4)|CRUSHING(56,10)|PHOSPHATE ESTER(52,8)|ANODE ELECTRODE(48,5)|PHOSPHATE 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COLLECTOR(19,1)|IMPURITY REMOVAL(19,1)|POLYOL VOLUME RATIO(19,1)|RECYCLED POSITIVE ELECTRODE MATERIAL(19,1)|BUTANOL(18,2)|POLE PIECE(17,2)|FLUORINE BLACK POWDER(16,10)|GLYCEROL(16,7)|ELECTRODE MATERIAL(16,6)|REDUCING AGENT(16,5)|CELL ELECTROLYTE INTERIOR(15,5)|PHOSPHATE MOLAR RATIO(15,5)|PROPYLENE GLYCOL(15,2)|MEMBRANE PROMOTING PYROLYSIS(15,1)|ETHYLENE GLYCOL(14,2)|SHEET ACTIVE SUBSTANCE(13,15)|GLUCOSE MIXING(13,4)|SOLID SOLUTION(13,4)|FERROUS OXALATE(12,6)|CHEMICAL COMPOSITION(12,2)|FERRITIC LITHIUM PHOSPHATE(12,2)|FLUORINE PYROLYSIS(12,1)|FRAGMENTATION SORTING(12,1)|LITHIUM CYCLING STABILITY(12,1)|CRUSHED BLOCK(11,5)|POLYVINYLIDENE FLUORIDE(11,5)|SOLUTION B(10,18)|COMBUSTION CHAMBER(10,10)|DISCHARGE CAPACITY(10,3)|ELECTROLYTE EXTRACTION(10,1)|FLUIDIZED BED PYROLYSIS(10,1)|HETEROLITHIUM HYDROXIDE(10,1)|LITHIUM FERRIC PHOSPHATE DIFFUSION(10,1)|LITHIUM MANGANATE(10,1)|MEMBRANE PYROLYSIS(10,1)|PYROLYSIS PROMOTION(10,1)|REPREPARED CELL FAILURE(10,1)|SINTERING FURNACE(10,1)|AREA RATIO(9,3)|BUCKLE CELL PERFORMANCE(9,2)|HEATING FURNACE(9,2)|SODIUM P TOLUENESULFONATE(8,7)|CALCIUM HYDROXIDE(8,6)|LITHIUM CARBONATE(8,6)|SEPARATION SOLUTION(8,6)|SOLAR RADIATION(8,6)|ACETYLENE BLACK(8,1)|DECARBURIZATION TREATMENT(8,1)|FERRIC HYDROXIDE(8,1)|LITHIUM NICKEL COBALT MANGANATE(8,1)|ROLLER KILN(8,1)|SNAP BATTERY(8,1)|PUMP AIR(7,5)|ELECTRODE SHEET(7,2)|HEATING TEMPERATURE(6,7)|BALL MILLING(6,4)|BINDER(6,4)|METAL SALT(6,4)|LICLO(6,3)|LIPF(6,3)|HEATING TUBE(6,2)|SOLID SOLUTION B(6,2)|BLACK POWDER DECARBURIZATION(6,1)|DECARBONIZATION(6,1)|FERROLITHIUM PHOSPHATE BATTERY INDUSTRY(6,1)|MAJOR CHALLENGE(6,1)|PEELING TREATMENT(6,1)|POST FLUORINE FLUOROCARBON CONTENT(6,1)|PYROLYZED BLACK POWDER(6,1)|SHREDDED PIECE(6,1)|SOLID B(5,7)|RECOVERY COST(5,4)|ABSCISSA(5,1)|ALUMINUM COPPER FOIL(5,1)|BREAKING SPEED(5,1)||(GB2620690)|BLACK POWDER(100,57)|LITHIUM IRON PHOSPHATE(100,54)|FLUORINE(100,48)|SOLID(100,41)|LITHIUM IRON PHOSPHATE BATTERY(100,38)|CRUSHED PIECE(100,26)|CARBON(100,24)|RECYCLING(100,14)|SOLID LIQUID SEPARATION(100,14)|BENZENE SULFONATE(100,11)|FLUIDIZED BED(100,10)|ELECTROLYTE(100,9)|PRECIPITATION(100,7)|BASE ADDITION(100,2)|POSITIVE ELECTRODE(100,1)|WASTE POLYANION BATTERY(100,1)|PHOSPHO ESTER(65,8)|CRUSHED SHELL(64,1)|ALUMINUM CRUSHING(62,1)|PHOSPHO MONOESTER(58,2)|PHOSPHO TRIESTER(52,2)|LITHIUM SUPPLEMENT(50,2)|CRUSHED CURRENT COLLECTOR(37,1)|COPPER FOIL(35,7)|STRIPPING LIQUID(34,21)|CRUSHING(31,4)|BATTERY MATERIAL RECYCLING(30,1)|CATHODE(27,16)|DIAPHRAGM(26,3)|PRIMARY HEAT(25,5)|PHOSPHODIESTER(25,2)|CATHODE CHEMICAL COMPONENT(23,1)|PRETREATING BATTERY(22,5)|ZINC BENZENESULFONATE(22,2)|ISOPROPANOL(21,2)|PHOSPHATE RADICAL(20,6)|SODIUM BENZENESULFONATE(19,2)|TRIMETHYL PHOSPHATE(19,2)|BUTANOL(17,2)|TRIETHYL PHOSPHATE(16,7)|IRON SUPPLEMENT(16,3)|DRY ELECTROLYTE(15,5)|FLUIDIZED BED PUMP(15,5)|NEON ENVIRONMENT(15,5)|REMOVING IMPURITY(15,5)|MEMBRANE PYROLYSIS(15,2)|PROPYLENE GLYCOL(15,2)|STRIPPING(15,2)|MOLAR RATIO(14,11)|CRUSHED PIECE AREA RATIO(14,8)|POLYOL VOLUME RATIO(14,3)|ETHYLENE GLYCOL(14,2)|FERROUS OXALATE(12,6)|REGENERATED LITHIUM IRON PHOSPHATE(12,6)|SEPARATION LIQUID(11,11)|EVAPORATED SOLID(11,5)|POLYVINYLIDENE FLUORIDE(11,5)|HEATING FURNACE(11,3)|CHEMICAL COMPONENT(11,1)|FLUORINE PYROLYSIS(11,1)|RECYCLING COST(10,4)|FLUIDIZED BED PYROLYSIS(10,1)|SINTERING FURNACE(10,1)|SEM GRAPH(9,2)|SODIUM P TOLUENESULFONATE(8,8)|CALCIUM HYDROXIDE(8,6)|GLUCOSE(8,6)|LITHIUM CARBONATE(8,6)|SOLAR RADIATION(8,6)|HEAT PIPE(8,2)|ACETYLENE BLACK(8,1)|FERRIC HYDROXIDE(8,1)|BALL MILLING(7,5)|COMBUSTION CHAMBER(7,5)|HEATER(7,5)|HEATING TEMPERATURE(7,5)|PROPANETRIOL VOLUME RATIO(7,5)|PUMP AIR(7,5)|REGENERATING CATHODE MATERIAL(7,5)|DISCHARGE CAPACITY(7,2)|PLATE ACTIVE SUBSTANCE(6,15)|BINDER(6,4)|LIPF(6,4)|MAH(6,4)|METAL SALT(6,4)|BATTERY ASSEMBLY(6,1)|CONVEYING CAPACITY(6,1)|STRIPPING TREATMENT(6,1)|WORKING VOLTAGE PLATFORM(6,1)|BLACK POWDER FLUORINE CONTENT(5,1)|CAPACITY DENSITY(5,1)|CLEAN ALUMINUM FOIL(5,1)|ELASTIC SHEET(5,1)|FERRIC CITRATE(5,1)|FERRIC OXALATE(5,1)|FERROUS CITRATE(5,1)||(GB2620690)|BLACK POWDER(100,57)|LITHIUM IRON PHOSPHATE(100,54)|FLUORINE(100,48)|SOLID(100,41)|LITHIUM IRON PHOSPHATE BATTERY(100,38)|CRUSHED PIECE(100,26)|CARBON(100,24)|RECYCLING(100,14)|SOLID LIQUID SEPARATION(100,14)|BENZENE SULFONATE(100,11)|FLUIDIZED BED(100,10)|ELECTROLYTE(100,9)|PRECIPITATION(100,7)|BASE ADDITION(100,2)|POSITIVE ELECTRODE(100,1)|WASTE POLYANION BATTERY(100,1)|PHOSPHO ESTER(65,8)|CRUSHED SHELL(64,1)|ALUMINUM CRUSHING(62,1)|PHOSPHO MONOESTER(58,2)|PHOSPHO TRIESTER(52,2)|LITHIUM SUPPLEMENT(50,2)|CRUSHED CURRENT COLLECTOR(37,1)|COPPER FOIL(35,7)|STRIPPING LIQUID(34,21)|CRUSHING(31,4)|BATTERY MATERIAL RECYCLING(30,1)|CATHODE(27,16)|DIAPHRAGM(26,3)|PRIMARY HEAT(25,5)|PHOSPHODIESTER(25,2)|CATHODE CHEMICAL COMPONENT(23,1)|PRETREATING BATTERY(22,5)|ZINC BENZENESULFONATE(22,2)|ISOPROPANOL(21,2)|PHOSPHATE RADICAL(20,6)|SODIUM BENZENESULFONATE(19,2)|TRIMETHYL PHOSPHATE(19,2)|BUTANOL(17,2)|TRIETHYL PHOSPHATE(16,7)|IRON SUPPLEMENT(16,3)|DRY ELECTROLYTE(15,5)|FLUIDIZED BED PUMP(15,5)|NEON ENVIRONMENT(15,5)|REMOVING IMPURITY(15,5)|MEMBRANE PYROLYSIS(15,2)|PROPYLENE GLYCOL(15,2)|STRIPPING(15,2)|MOLAR RATIO(14,11)|CRUSHED PIECE AREA RATIO(14,8)|POLYOL VOLUME RATIO(14,3)|ETHYLENE GLYCOL(14,2)|FERROUS OXALATE(12,6)|REGENERATED LITHIUM IRON PHOSPHATE(12,6)|SEPARATION LIQUID(11,11)|EVAPORATED SOLID(11,5)|POLYVINYLIDENE FLUORIDE(11,5)|HEATING FURNACE(11,3)|CHEMICAL COMPONENT(11,1)|FLUORINE PYROLYSIS(11,1)|RECYCLING COST(10,4)|FLUIDIZED BED PYROLYSIS(10,1)|SINTERING FURNACE(10,1)|SEM GRAPH(9,2)|SODIUM P TOLUENESULFONATE(8,8)|CALCIUM HYDROXIDE(8,6)|GLUCOSE(8,6)|LITHIUM CARBONATE(8,6)|SOLAR RADIATION(8,6)|HEAT PIPE(8,2)|ACETYLENE BLACK(8,1)|FERRIC HYDROXIDE(8,1)|BALL MILLING(7,5)|COMBUSTION CHAMBER(7,5)|HEATER(7,5)|HEATING TEMPERATURE(7,5)|PROPANETRIOL VOLUME RATIO(7,5)|PUMP AIR(7,5)|REGENERATING CATHODE MATERIAL(7,5)|DISCHARGE CAPACITY(7,2)|PLATE ACTIVE SUBSTANCE(6,15)|BINDER(6,4)|LIPF(6,4)|MAH(6,4)|METAL SALT(6,4)|BATTERY ASSEMBLY(6,1)|CONVEYING CAPACITY(6,1)|STRIPPING TREATMENT(6,1)|WORKING VOLTAGE PLATFORM(6,1)|BLACK POWDER FLUORINE CONTENT(5,1)|CAPACITY DENSITY(5,1)|CLEAN ALUMINUM FOIL(5,1)|ELASTIC SHEET(5,1)|FERRIC CITRATE(5,1)|FERRIC OXALATE(5,1)|FERROUS CITRATE(5,1)||(GB2620690)|BLACK POWDER(100,57)|LITHIUM IRON PHOSPHATE(100,54)|FLUORINE(100,48)|SOLID(100,41)|LITHIUM IRON PHOSPHATE BATTERY(100,38)|CRUSHED PIECE(100,26)|CARBON(100,24)|RECYCLING(100,14)|SOLID LIQUID SEPARATION(100,14)|BENZENE SULFONATE(100,11)|FLUIDIZED BED(100,10)|ELECTROLYTE(100,9)|PRECIPITATION(100,7)|BASE ADDITION(100,2)|POSITIVE ELECTRODE(100,1)|WASTE POLYANION BATTERY(100,1)|PHOSPHO ESTER(65,8)|CRUSHED SHELL(64,1)|ALUMINUM CRUSHING(62,1)|PHOSPHO MONOESTER(58,2)|PHOSPHO TRIESTER(52,2)|LITHIUM SUPPLEMENT(50,2)|CRUSHED CURRENT COLLECTOR(37,1)|COPPER FOIL(35,7)|STRIPPING LIQUID(34,21)|CRUSHING(31,4)|BATTERY MATERIAL RECYCLING(30,1)|CATHODE(27,16)|DIAPHRAGM(26,3)|PRIMARY HEAT(25,5)|PHOSPHODIESTER(25,2)|CATHODE CHEMICAL COMPONENT(23,1)|PRETREATING BATTERY(22,5)|ZINC BENZENESULFONATE(22,2)|ISOPROPANOL(21,2)|PHOSPHATE RADICAL(20,6)|SODIUM BENZENESULFONATE(19,2)|TRIMETHYL PHOSPHATE(19,2)|BUTANOL(17,2)|TRIETHYL PHOSPHATE(16,7)|IRON SUPPLEMENT(16,3)|DRY ELECTROLYTE(15,5)|FLUIDIZED BED PUMP(15,5)|NEON ENVIRONMENT(15,5)|REMOVING IMPURITY(15,5)|MEMBRANE PYROLYSIS(15,2)|PROPYLENE GLYCOL(15,2)|STRIPPING(15,2)|MOLAR RATIO(14,11)|CRUSHED PIECE AREA RATIO(14,8)|POLYOL VOLUME RATIO(14,3)|ETHYLENE GLYCOL(14,2)|FERROUS OXALATE(12,6)|REGENERATED LITHIUM IRON PHOSPHATE(12,6)|SEPARATION LIQUID(11,11)|EVAPORATED SOLID(11,5)|POLYVINYLIDENE FLUORIDE(11,5)|HEATING FURNACE(11,3)|CHEMICAL COMPONENT(11,1)|FLUORINE PYROLYSIS(11,1)|RECYCLING COST(10,4)|FLUIDIZED BED PYROLYSIS(10,1)|SINTERING FURNACE(10,1)|SEM GRAPH(9,2)|SODIUM P TOLUENESULFONATE(8,8)|CALCIUM HYDROXIDE(8,6)|GLUCOSE(8,6)|LITHIUM CARBONATE(8,6)|SOLAR RADIATION(8,6)|HEAT PIPE(8,2)|ACETYLENE BLACK(8,1)|FERRIC HYDROXIDE(8,1)|BALL MILLING(7,5)|COMBUSTION CHAMBER(7,5)|HEATER(7,5)|HEATING TEMPERATURE(7,5)|PROPANETRIOL VOLUME RATIO(7,5)|PUMP AIR(7,5)|REGENERATING CATHODE MATERIAL(7,5)|DISCHARGE CAPACITY(7,2)|PLATE ACTIVE SUBSTANCE(6,15)|BINDER(6,4)|LIPF(6,4)|MAH(6,4)|METAL SALT(6,4)|BATTERY ASSEMBLY(6,1)|CONVEYING CAPACITY(6,1)|STRIPPING TREATMENT(6,1)|WORKING VOLTAGE PLATFORM(6,1)|BLACK POWDER FLUORINE CONTENT(5,1)|CAPACITY DENSITY(5,1)|CLEAN ALUMINUM FOIL(5,1)|ELASTIC SHEET(5,1)|FERRIC CITRATE(5,1)|FERRIC OXALATE(5,1)|FERROUS CITRATE(5,1)||(DE112022000199)|LITHIUM IRON PHOSPHATE(100,68)|LITHIUM IRON PHOSPHATE BATTERY(100,36)|RECYCLING(100,17)|CATHODE(100,16)|CRUSHED PIECE(100,8)|POSITIVE ELECTRODE(100,1)|LITHIUM ADDITIVE(68,4)|PHOSPHO ESTER(59,8)|IRON ADDITIVE(58,4)|BASE ADDITION(51,2)|PHOSPHO MONOESTER(47,2)|PHOSPHO TRIESTER(47,2)|BLACK POWDER(46,61)|WASTE BATTERIE(46,9)|FLUORINE(43,48)|ELECTROLYTE(43,14)|BENZENE SULFONATE(39,5)|PHOSPHATE RADICAL(38,7)|PURIFICATION(38,1)|PRECIPITATE(33,5)|MIX COPPER ALUMINUM(33,1)|COMMINUTED PIECE(32,20)|POLYOL(32,6)|STRIPPING LIQUID(31,23)|RECYCLING COST(30,3)|CATHODE PRODUCTION(30,2)|FLUIDIZED BED(29,6)|COMMINUTION(29,3)|STRIPPING TREATMENT(29,2)|BATTERY MATERIAL RECYCLING(27,1)|CARBOTHERMAL REDUCTION(27,1)|STRIPPING(25,2)|RECYCLING(24,1)|PRIMARY HEAT(22,5)|PURITY(22,3)|PHOSPHODIESTER(22,2)|CATHODE CHEMICAL COMPONENT(21,1)|BATTERY PRETREATMENT(20,5)|COMMINUTION(20,3)|SHELL(20,3)|ZINC BENZENESULFONATE(20,2)|SOLID LIQUID SEPARATION(19,18)|BINDER(19,4)|RECYCLED CATHODE MATERIAL(19,4)|ISOPROPANOL(19,2)|CATHODE MATERIAL(18,27)|LITHIUM(18,13)|COPPER FOIL(17,8)|SODIUM BENZENESULFONATE(17,2)|TRIMETHYL PHOSPHATE(17,2)|BUTANOL(16,2)|CURRENT COLLECTOR(16,1)|USED POLYANION BATTERY COMMINUTION(16,1)|TRIETHYL PHOSPHATE(15,7)|REDUCING AGENT(14,5)|MEMBRANE PYROLYSIS(14,2)|PROPYLENE GLYCOL(14,2)|FLUIDIZED BED PUMP(13,5)|NEON ENVIRONMENT(13,5)|MOLAR RATIO(12,11)|ETHYLENE GLYCOL(12,2)|LYE OXIDIZATION(12,2)|OXIDIZED LYE PH(12,1)|PLATELET SHAPED ACTIVE INGREDIENT(11,15)|REGENERATED LITHIUM IRON PHOSPHATE(11,6)|EVAPORATED SOLID(10,5)|POLYVINYLIDENE FLUORIDE(10,5)|PRECIPITATION(10,5)|RECYCLED LITHIUM IRON PHOSPHATE(10,5)|CARBON 016AFTER REMOVAL(10,3)|HEATING FURNACE(10,3)|REMOVING IMPURITY(10,3)|CHEMICAL COMPONENT(10,1)|FLUORINE PYROLYSIS(10,1)|USED POLYANION BATTERY(10,1)|ELECTROLYTE EXTRACTION(9,1)|FLUIDIZED BED PYROLYSIS(9,1)|SEM PHOTOGRAPH(9,1)|SINTERING FURNACE(9,1)|SOLAR IRRADIATION(9,1)|MAH(8,8)|TECHNOLOGICAL CONDITION(8,2)|SODIUM P TOLUENESULFONATE(7,8)|BALL MILLING(7,6)|CALCIUM HYDROXIDE(7,6)|GLUCOSE(7,6)|LITHIUM CARBONATE(7,6)|IRON PHOSPHATE CRYSTAL(7,3)|IRON PHOSPHATE FILTER RESIDUE(7,3)|IRON PHOSPHATE WASTE(7,3)|LITHIUM IRON PHOSPHATE POWDER(7,3)|ACETYLENE BLACK(7,1)|ALUMINUM COMMINUTION(7,1)|EXECUTIONCARBON CONTENT(7,1)|FIRING FURNACE(7,1)|INSOLUBLE SUBSTANCE(7,1)|OLD BATTERY(7,1)|RECYCLING TREATMENT(7,1)|COMBUSTION CHAMBER(6,5)|HEATER(6,5)|HEATING TEMPERATURE(6,5)|PROPANETRIOL VOLUME RATIO(6,5)|PUMP AIR(6,5)|SOLAR RADIATION(6,5)|LIPF(6,4)|ALUMINUM COPPER WASTE(6,2)|BLACK POWDER FLUORINE CONTENT(6,2)|0087OF CARBON(6,1)|ALKALINE SUBSTANCE(6,1)|BALL MILLED POWDER(6,1)|BUTTON BATTERY ASSEMBLY(6,1)|CARBON 015AFTER REMOVAL(6,1)|CARBON 018AFTER REMOVAL(6,1)|CARBON 019AFTER REMOVAL(6,1)|CHARGING LIFE(6,1)|CONVEYING CAPACITY(6,1)|DEMOUNTING(6,1)|DISASSEMBLING(6,1)|DISCHARGE CAPACITANCE(6,1)|LATE REMOVAL(6,1)|PYROLYZING BLACK POWDER(6,1)|QUALIFIED LITHIUM IRON PHOSPHATE(6,1)|TUBULAR FURNACE(6,1)|ACIDIC SOLUTION(5,3)|OXIDIZING AGENT(5,3)|HEATING TUBE(5,2)|BATTERY COMPATIBLE IRON PHOSPHATE(4,1)|BATTERY PRODUCTION(4,1)|BLACK LITHIUM IRON PHOSPHATE(4,1)|CAPACITY DENSITY(4,1)|CLASSIFICATION(4,1)|CLEAN ALUMINUM FOIL(4,1)|CYCLE STABILITY(4,1)|ELASTIC FILM(4,1)|FRUCTOSE(4,1)|LITHIUM ION BUTTON BATTERY(4,1)|LITHIUM IRON PHOSPHATE CATHODE(4,1)|LITHIUM IRON PHOSPHATE ELECTRODE(4,1)|LITHIUM IRON PHOSPHATE PRECURSOR(4,1)|MUFFLE FURNACE(4,1)||(DE112022000199)|LITHIUM IRON PHOSPHATE(100,68)|LITHIUM IRON PHOSPHATE BATTERY(100,36)|RECYCLING(100,17)|CATHODE(100,16)|CRUSHED PIECE(100,8)|POSITIVE ELECTRODE(100,1)|LITHIUM ADDITIVE(68,4)|PHOSPHO ESTER(59,8)|IRON ADDITIVE(58,4)|BASE ADDITION(51,2)|PHOSPHO MONOESTER(47,2)|PHOSPHO TRIESTER(47,2)|BLACK POWDER(46,61)|WASTE BATTERIE(46,9)|FLUORINE(43,48)|ELECTROLYTE(43,14)|BENZENE SULFONATE(39,5)|PHOSPHATE RADICAL(38,7)|PURIFICATION(38,1)|PRECIPITATE(33,5)|MIX COPPER ALUMINUM(33,1)|COMMINUTED PIECE(32,20)|POLYOL(32,6)|STRIPPING LIQUID(31,23)|RECYCLING COST(30,3)|CATHODE PRODUCTION(30,2)|FLUIDIZED BED(29,6)|COMMINUTION(29,3)|STRIPPING TREATMENT(29,2)|BATTERY MATERIAL RECYCLING(27,1)|CARBOTHERMAL REDUCTION(27,1)|STRIPPING(25,2)|RECYCLING(24,1)|PRIMARY HEAT(22,5)|PURITY(22,3)|PHOSPHODIESTER(22,2)|CATHODE CHEMICAL COMPONENT(21,1)|BATTERY PRETREATMENT(20,5)|COMMINUTION(20,3)|SHELL(20,3)|ZINC BENZENESULFONATE(20,2)|SOLID LIQUID SEPARATION(19,18)|BINDER(19,4)|RECYCLED CATHODE MATERIAL(19,4)|ISOPROPANOL(19,2)|CATHODE MATERIAL(18,27)|LITHIUM(18,13)|COPPER FOIL(17,8)|SODIUM BENZENESULFONATE(17,2)|TRIMETHYL PHOSPHATE(17,2)|BUTANOL(16,2)|CURRENT COLLECTOR(16,1)|USED POLYANION BATTERY COMMINUTION(16,1)|TRIETHYL PHOSPHATE(15,7)|REDUCING AGENT(14,5)|MEMBRANE PYROLYSIS(14,2)|PROPYLENE GLYCOL(14,2)|FLUIDIZED BED PUMP(13,5)|NEON ENVIRONMENT(13,5)|MOLAR RATIO(12,11)|ETHYLENE GLYCOL(12,2)|LYE OXIDIZATION(12,2)|OXIDIZED LYE PH(12,1)|PLATELET SHAPED ACTIVE INGREDIENT(11,15)|REGENERATED LITHIUM IRON PHOSPHATE(11,6)|EVAPORATED SOLID(10,5)|POLYVINYLIDENE FLUORIDE(10,5)|PRECIPITATION(10,5)|RECYCLED LITHIUM IRON PHOSPHATE(10,5)|CARBON 016AFTER REMOVAL(10,3)|HEATING FURNACE(10,3)|REMOVING IMPURITY(10,3)|CHEMICAL COMPONENT(10,1)|FLUORINE PYROLYSIS(10,1)|USED POLYANION BATTERY(10,1)|ELECTROLYTE EXTRACTION(9,1)|FLUIDIZED BED PYROLYSIS(9,1)|SEM PHOTOGRAPH(9,1)|SINTERING FURNACE(9,1)|SOLAR IRRADIATION(9,1)|MAH(8,8)|TECHNOLOGICAL CONDITION(8,2)|SODIUM P TOLUENESULFONATE(7,8)|BALL MILLING(7,6)|CALCIUM HYDROXIDE(7,6)|GLUCOSE(7,6)|LITHIUM CARBONATE(7,6)|IRON PHOSPHATE CRYSTAL(7,3)|IRON PHOSPHATE FILTER RESIDUE(7,3)|IRON PHOSPHATE WASTE(7,3)|LITHIUM IRON PHOSPHATE POWDER(7,3)|ACETYLENE BLACK(7,1)|ALUMINUM COMMINUTION(7,1)|EXECUTIONCARBON CONTENT(7,1)|FIRING FURNACE(7,1)|INSOLUBLE SUBSTANCE(7,1)|OLD BATTERY(7,1)|RECYCLING TREATMENT(7,1)|COMBUSTION CHAMBER(6,5)|HEATER(6,5)|HEATING TEMPERATURE(6,5)|PROPANETRIOL VOLUME RATIO(6,5)|PUMP AIR(6,5)|SOLAR RADIATION(6,5)|LIPF(6,4)|ALUMINUM COPPER WASTE(6,2)|BLACK POWDER FLUORINE CONTENT(6,2)|0087OF CARBON(6,1)|ALKALINE SUBSTANCE(6,1)|BALL MILLED POWDER(6,1)|BUTTON BATTERY ASSEMBLY(6,1)|CARBON 015AFTER REMOVAL(6,1)|CARBON 018AFTER REMOVAL(6,1)|CARBON 019AFTER REMOVAL(6,1)|CHARGING LIFE(6,1)|CONVEYING CAPACITY(6,1)|DEMOUNTING(6,1)|DISASSEMBLING(6,1)|DISCHARGE CAPACITANCE(6,1)|LATE REMOVAL(6,1)|PYROLYZING BLACK POWDER(6,1)|QUALIFIED LITHIUM IRON PHOSPHATE(6,1)|TUBULAR FURNACE(6,1)|ACIDIC SOLUTION(5,3)|OXIDIZING AGENT(5,3)|HEATING TUBE(5,2)|BATTERY COMPATIBLE IRON PHOSPHATE(4,1)|BATTERY PRODUCTION(4,1)|BLACK LITHIUM IRON PHOSPHATE(4,1)|CAPACITY DENSITY(4,1)|CLASSIFICATION(4,1)|CLEAN ALUMINUM FOIL(4,1)|CYCLE STABILITY(4,1)|ELASTIC FILM(4,1)|FRUCTOSE(4,1)|LITHIUM ION BUTTON BATTERY(4,1)|LITHIUM IRON PHOSPHATE CATHODE(4,1)|LITHIUM IRON PHOSPHATE ELECTRODE(4,1)|LITHIUM IRON PHOSPHATE PRECURSOR(4,1)|MUFFLE FURNACE(4,1)||(CN114229816)|LITHIUM IRON PHOSPHATE(100,55)|LITHIUM IRON PHOSPHATE BATTERY(100,39)|POSITIVE ELECTRODE(100,16)|RECYCLING(100,6)|ANODE(100,1)|LITHIUM SUPPLEMENT(83,2)|RECOVERY COST(65,3)|ELECTROLYTE DRYING(61,2)|FLUORINE DECARBURIZATION(61,2)|POPULARIZATION(48,1)|BLACK POWDER(46,41)|CRUSHED BLOCK(45,9)|PERFORMANCE REQUIREMENT(45,1)|PHOSPHATE ESTER(42,6)|ALUMINUM COPPER FOIL(39,1)|RECYCLED ANODE MATERIAL PURITY(39,1)|BENZENE SULFONATE(36,11)|RECYCLING COST(36,2)|LITHIUM ADDITION(36,1)|REMOVING FLUORINE(35,5)|RECOVERED POSITIVE ELECTRODE MATERIAL(34,3)|RECYCLED ANODE MATERIAL(32,1)|OPTIMIZATION(31,1)|FLUIDIZED BED(30,11)|REMOVING IMPURITY(30,7)|PHOSPHORIC ACID MONOESTER(30,2)|PHOSPHORIC ACID TRIESTER(30,2)|STRIPPING LIQUID(29,21)|FLUORINE(29,13)|PRECIPITATE(29,7)|BROKEN FRAGMENT(29,4)|PHOSPHORIC ACID DIESTER(29,2)|ELECTRODE MATERIAL(28,7)|IRON SUPPLEMENT(26,3)|PRIMARY HEAT(25,6)|STRIPPING SOLUTION(25,3)|ACID ADDITION(24,1)|SEPARATION LIQUID(23,12)|BATTERY PRETREATMENT(23,5)|ZINC BENZENESULFONATE(23,2)|ISOPROPANOL(22,2)|FLAKY ACTIVE SUBSTANCE(20,15)|CARBOTHERMIC REDUCTION(19,2)|SODIUM BENZENESULFONATE(19,2)|TRIMETHYL PHOSPHATE(19,2)|BUTANOL(18,2)|TRIETHYL PHOSPHATE(17,7)|HIGH PURITY POSITIVE ELECTRODE(17,2)|SOLID LIQUID SEPARATION(16,14)|FLUORINE BLACK POWDER(16,10)|REDUCING AGENT(16,5)|POLYOL VOLUME RATIO(16,3)|FLUIDIZED BED PUMP(15,5)|NEON ENVIRONMENT(15,5)|FLUOROCARBON CONTENT(15,3)|PROPYLENE GLYCOL(15,2)|CATHODE MATERIAL(14,6)|ETHYLENE GLYCOL(14,2)|WASTE POLYANION BATTERY(13,1)|ALUMINUM COPPER(12,6)|HEATING FURNACE(12,3)|BROKEN PIECE AREA RATIO(12,1)|CRUSHED SHELL INFLUENCE(12,1)|REGENERATED LITHIUM IRON PHOSPHATE(11,5)|SIEVING(11,5)|BATTERY MATERIAL RECOVERY(11,2)|COMBUSTION CHAMBER(10,10)|FERROUS OXALATE(10,4)|5C MAGNIFICATION(10,1)|EXTRACTING ELECTROLYTE(10,1)|SEPARATION(10,1)|SINTERING FURNACE(10,1)|SUBSTANCE PYROLYSIS(10,1)|PHOSPHATE RADICAL MOLAR RATIO(9,2)|SODIUM P TOLUENESULFONATE(8,8)|CALCIUM HYDROXIDE(8,6)|GLUCOSE(8,6)|GRINDING(8,6)|LITHIUM CARBONATE(8,6)|SOLAR RADIATION(8,6)|HEAT PIPE(8,2)|ACETYLENE BLACK(8,1)|FERRIC HYDROXIDE(8,1)|FLUIDIZED BED PYROLYSIS MODE(8,1)|INDUSTRIAL APPLICATION(8,1)|LITHIUM ANODE(8,1)|NICKEL COBALT LITHIUM MANGANATE(8,1)|POLYVINYLIDENE FLUORIDE ETHYLENE(8,1)|PREPARED ELECTRODE SLICE(8,1)|ROLLER KILN(8,1)|BALL MILLING(7,5)|GLYCEROL VOLUME RATIO(7,5)|HEATER(7,5)|PH VALUE(7,5)|PUMPING AIR(7,5)|STANDBY(7,5)|BLACK POWDER MEDIUM DIAPHRAGM(7,2)|DISCHARGE CAPACITY(7,2)|SEM IMAGE(7,2)|HEATING TEMPERATURE(6,7)|METAL SALT(6,4)|LIPF(6,3)|ASSEMBLED BATTERY DISCHARGING PERFORMANCE(6,1)|BATTERY ASSEMBLY(6,1)|BLACK POWDER DECARBURIZATION(6,1)|BLACK POWDER FLUORINATION(6,1)|CONVEYING CAPACITY(6,1)|DECARBONIZATION(6,1)|FLUORINE TREATMENT(6,1)|LATE REMOVAL(6,1)|RECOVERY TREATMENT(6,1)|STRIPPING TREATMENT(6,1)|WORKING VOLTAGE PLATFORM(6,1)|ABSCISSA(5,1)|ALUMINUM COPPER DEBRIS(5,1)|BENZENE SULFONATE THERMAL DECOMPOSITION(5,1)|BLACK POWDER FLUORINE REMOVAL(5,1)|BUTTON CELL BATTERIE(5,1)|CAPACITY DENSITY(5,1)|CLEAN ALUMINUM FOIL(5,1)|CRUSHED CURRENT COLLECTOR(5,1)||(CN114229816)|LITHIUM IRON PHOSPHATE(100,56)|LITHIUM IRON PHOSPHATE BATTERY(100,39)|POSITIVE ELECTRODE(100,15)|RECYCLING(100,4)|ANODE(100,1)|LITHIUM SUPPLEMENT(78,2)|RECOVERY COST(65,3)|ELECTROLYTE DRYING(61,2)|FLUORINE DECARBURIZATION(61,2)|POPULARIZATION(48,1)|BLACK POWDER(47,41)|CRUSHED BLOCK(45,9)|PERFORMANCE REQUIREMENT(45,1)|PHOSPHATE ESTER(42,6)|ALUMINUM COPPER FOIL(39,1)|POLYOL(38,7)|BENZENE SULFONATE(36,11)|RECYCLING COST(36,2)|LITHIUM ADDITION(36,1)|REMOVING FLUORINE(35,5)|STRIPPING LIQUID(34,17)|RECOVERED POSITIVE ELECTRODE MATERIAL(34,3)|PURITY(34,1)|RECYCLED ANODE MATERIAL(32,1)|OPTIMIZATION(31,1)|FLUIDIZED BED(30,11)|REMOVING IMPURITY(30,7)|PHOSPHORIC ACID MONOESTER(30,2)|PHOSPHORIC ACID TRIESTER(30,2)|FLUORINE(29,13)|PRECIPITATE(29,7)|BROKEN FRAGMENT(29,4)|PHOSPHORIC ACID DIESTER(29,2)|PHOSPHATE RADICAL(28,11)|ELECTRODE MATERIAL(28,7)|IRON SUPPLEMENT(26,3)|PRIMARY HEAT(25,6)|BROKEN PIECE(24,12)|STRIPPING SOLUTION(24,6)|ACID ADDITION(24,1)|SEPARATION LIQUID(23,9)|BATTERY PRETREATMENT(23,5)|ZINC BENZENESULFONATE(23,2)|ISOPROPANOL(22,2)|CARBOTHERMIC REDUCTION(19,2)|SODIUM BENZENESULFONATE(19,2)|TRIMETHYL PHOSPHATE(19,2)|FLAKY ACTIVE SUBSTANCE(18,13)|BUTANOL(18,2)|TRIETHYL PHOSPHATE(17,7)|HIGH PURITY POSITIVE ELECTRODE(17,2)|SOLID LIQUID SEPARATION(16,14)|FLUORINE BLACK POWDER(16,10)|GLYCEROL(16,6)|REDUCING AGENT(16,5)|PROPYLENE GLYCOL(15,2)|CATHODE MATERIAL(14,7)|SIZE ETHYLENE GLYCOL(13,1)|WASTE POLYANION BATTERY(13,1)|ALUMINUM COPPER(12,6)|FERROUS OXALATE(12,6)|HEATING FURNACE(12,3)|POSITIVE ELECTRODE6THE ELECTROLYTE(12,1)|POLYVINYLIDENE FLUORIDE(11,5)|REGENERATED LITHIUM IRON PHOSPHATE(11,5)|BATTERY MATERIAL RECOVERY(11,2)|COMBUSTION CHAMBER(10,10)|5C MAGNIFICATION(10,1)|CRUSHING SHELL(10,1)|EXTRACTING ELECTROLYTE(10,1)|PREPARETHE ELECTRODE(10,1)|SEPARATION(10,1)|SINTERING FURNACE(10,1)|AREA RATIO(9,3)|CALCIUM HYDROXIDE(8,6)|GRINDING(8,6)|LITHIUM CARBONATE(8,6)|SOLAR RADIATION(8,6)|HEAT PIPE(8,2)|ACETYLENE BLACK(8,1)|ELECTRODE SLICE(8,1)|FERRIC HYDROXIDE(8,1)|FLUIDIZED BED PYROLYSIS MODE(8,1)|INDUSTRIAL APPLICATION(8,1)|NEON FILLED GLOVE BOX(8,1)|NICKEL COBALT LITHIUM MANGANATE(8,1)|ROLLER KILN(8,1)|VOLUME RATIO(7,8)|BALL MILLING(7,5)|HEATER(7,5)|HEATING EQUIPMENT(7,5)|HEATING TEMPERATURE(7,5)|PH VALUE(7,5)|PUMPING AIR(7,5)|SEPARATION SOLUTION(7,5)|STANDBY(7,5)|BLACK POWDER MEDIUM DIAPHRAGM(7,2)|DISCHARGE CAPACITY(7,2)|FLUORINATION(7,2)|SEM IMAGE(7,2)|SIZE SODIUM P TOLUENESULFONATE(7,2)|CONTENT SIZE FLUOROCARBON(6,3)|CRUSHING(6,3)|PROCESS SIZE(6,2)|BATTERY ASSEMBLY(6,1)|BLACK POWDER DECARBURIZATION(6,1)|CONVEYING CAPACITY(6,1)|DECARBONIZATION(6,1)|FLUORINE TREATMENT(6,1)|LATE REMOVAL(6,1)|RECOVERY TREATMENT(6,1)|STRIPPING TREATMENT(6,1)|WORKING VOLTAGE PLATFORM(6,1)|ABSCISSA(5,1)|ALUMINUM COPPER DEBRIS(5,1)|BUTTON CELL BATTERIE(5,1)| (US12009492)|The invention claimed is:|1. A method for recycling and preparing a cathode material from waste lithium iron phosphate batteries, comprising:| (1) discharging the waste lithium iron phosphate batteries, drying an electrolyte inside the waste lithium iron phosphate batteries, then crushing to obtain crushed pieces, and stripping the crushed pieces to obtain a black powder;| (2) mixing the black powder obtained in step (1) with a benzene sulfonate, and then reacting in a fluidized bed to obtain a black powder with carbon and fluorine being removed;| (3) adding an acid into the black powder with carbon and fluorine being removed in step (2), performing solid-liquid separation to obtain a solution A and a solid A; and then, adding an alkali into the solution A until no precipitation is generated, and performing solid-liquid separation to obtain a solution B and a solid B; and| (4) mixing the solid A and the solution B obtained in step (3), adding at least one of a lithium supplement agent, an iron supplement agent or a phosphate to obtain a mixture, then adding a reducing agent into the mixture, and sintering to obtain the cathode material.|2. The method of claim 1, wherein in step (1), an area ratio of the crushed pieces to the waste lithium iron phosphate batteries is greater than 5%.|3. The method of claim 1, wherein in step (1), the stripping comprises placing the crushed pieces in a stripping liquid, performing primary heating, and separating into a solid and a separated liquid; and then subjecting the separated liquid to secondary heating, and removing the stripping liquid to obtain the black powder.|4. The method of claim 3, wherein the stripping liquid comprises polyol and phosphoester.|5. The method of claim 4, wherein the polyol is selected from at least one of ethylene glycol, propylene glycol, propanetriol, 1,2-butanediol or 1,3-butanediol; and the phosphoester is selected from at least one of phosphomonoester, phosphodiester, phosphotriester, triethyl phosphate or trimethyl phosphate.|6. The method of claim 5, wherein a volume ratio of the polyol to the phosphoester is 1:(0.1 to 1).|7. The method of claim 4, wherein a volume ratio of the polyol to the phosphoester is 1:(0.1 to 1).|8. The method of claim 3, wherein the primary heating is performed at a temperature of 130° C. to 210° C., and the primary heating lasts for 0.5 hour to 10 hours; and the secondary heating is performed at a temperature of 210° C. to 300° ° C., and the secondary heating lasts for 2 hours to 12 hours.|9. The method of claim 1, wherein in step (2), an addition amount of the benzene sulfonate is 0.1 w % to 5 w % of the black powder.|10. The method of claim 9, wherein in step (2), the benzene sulfonate is selected from at least one of sodium p-toluenesulfonate, sodium benzenesulfonate or zinc benzenesulfonate.|11. The method of claim 1, wherein in step (2), the reacting is performed at a temperature of 300° ° C. to 850° C., and lasts for 1 minute to 360 minutes. (US12009492)|CROSS-REFERENCE TO RELATED APPLICATION|[0001] This application is a national stage filing under 35 U.S.C. § 371 of international application number PCT/CN2022/111816, filed Aug. 11, 2022, which claims priority to Chinese patent application No. 202111367677.5, filed Nov. 18, 2021. The contents of these applications are incorporated herein by reference in their entirety.|(US12009492)|TECHNICAL FIELD|[0002] The present disclosure relates to the technical field of recycling battery materials, and particularly, to a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery.|BACKGROUND|[0003] Although lithium iron phosphate batteries are inferior to those of the same type of transition metal oxide batteries, such as lithium nickel cobalt manganese and lithium manganese, in working voltage platform and capacity density, the lithium iron phosphate batteries are superior to the transition metal oxide batteries in charge and discharge cycle life, safety, thermal stability and manufacturing cost. Therefore, under the demands for long life, low cost and easy use of batteries, the lithium iron phosphate batteries have become a preferred choice for electric energy storage and power batteries. With the development of the lithium iron phosphate battery industry, it can be expected that a large number of waste lithium iron phosphate batteries will be replaced in the future. Therefore, how to deal with and recycle the waste lithium iron phosphate batteries will also become a big problem.|[0004] Currently, recycling the waste lithium iron phosphate batteries generally includes the following steps of: classifying the waste lithium iron phosphate battery according to chemical compositions of the battery, then physically dismounting the waste lithium iron phosphate battery, then performing high-temperature calcination and crushing for separation, and extracting the electrolyte. There are still some problems in this recycling method, for example, during mechanical crushing, waste polyanion batteries may be affected by crushed shells and crushed current collectors and diaphragms, so as to change physical and chemical components of a cathode material to be recycled. On one hand, the crushing process destroys an internal crystal arrangement of the cathode material. On the other hand, the crushing process mixes copper-aluminum and phosphate radical with the electrolyte and the binder together, which increases the difficulty of subsequent purification. Especially, the crushing of aluminum and copper foils makes the aluminum and copper foils be mixed with each other, and the mixture cannot be separated accurately by mechanical separation. Therefore, the recycling cost is high, and the purity of the recycled cathode material is low, and the batteries prepared again cannot meet performance requirements, which also limit the industrial application and popularization of the lithium iron phosphate battery to a certain extent.|[0005] Therefore, it is urgent to provide a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery, which can recycle and obtain a cathode material with high purity while controlling the recycling cost, and batteries prepared again by using the recycled cathode material have good performances.|SUMMARY|[0006] The present disclosure aims at solving at least one of the above-mentioned technical problems in the prior art. Therefore, the present disclosure proposes a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery, which can recycle and obtain a cathode material with high purity while controlling the recycling cost, and batteries prepared again by using the recycled cathode material have good performances.|[0007] The present disclosure provides a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery.|[0008] Specifically, the method for recycling and preparing the cathode material from the waste lithium iron phosphate battery includes the following steps of:| - (1) discharging a waste lithium iron phosphate battery, drying an electrolyte inside the waste lithium iron phosphate battery, then crushing to obtain crushed pieces, and stripping the crushed pieces to obtain a black powder;| - (2) mixing the black powder obtained in step (1) with benzene sulfonate, and then reacting in a fluidized bed to obtain a black powder without carbon and fluorine removed;| - (3) adding acid into the black powder without carbon and fluorine removed in step (2) for solid-liquid separation to obtain a solution A and a solid A; and then, adding alkali into the solution A until no precipitation is generated, and performing solid-liquid separation to obtain a solution B and a solid B; and| - (4) mixing the solid A and the solution B obtained in step (3), adding at least one of a lithium supplement agent, an iron supplement agent or phosphate to obtain a mixture, then adding a reducing agent into the mixture, and sintering to obtain a cathode material.|[0013] Preferably, in step (1), the discharging process is that the waste lithium iron phosphate battery is placed in a solution of metal salt and discharged for 0.1 day to 10 days.|[0014] Preferably, the metal salt is selected from one or more of sodium chloride, sodium sulfate, sodium phosphate, magnesium chloride, magnesium sulfate, lithium sulfate or lithium chloride.|[0015] Preferably, in the solution of the metal salt, a mass concentration of the metal salt respectively ranges from 0.1 w % to 20 w %.|[0016] Preferably, in step (1), the drying process is that the waste lithium iron phosphate battery is placed in a sintering furnace, a kiln, a muffle furnace, an electric furnace or an oven and dried at 15° C. to 150° C. for 1 hour to 120 hours. Alternatively, the waste lithium iron phosphate battery may be placed under solar radiation.|[0017] Preferably, in step (1), the crushing process is that the waste lithium iron phosphate battery is sheared for 1 times to 10 times to obtain the crushed pieces.|[0018] Preferably, an area ratio of the crushed pieces to the waste lithium iron phosphate battery is greater than 5%; and further preferably, the area ratio of the crushed pieces to the waste lithium iron phosphate battery is greater than 10%.|[0019] Preferably, in step (1), the stripping process is that the crushed pieces are placed in a stripping liquid, subjected to primary heating, and separated into a solid and a separated liquid; and then, the separated liquid is subjected to secondary heating, and the stripping liquid is removed to obtain the black powder. The solid refers to aluminum and copper foils which are recycled after separation.|[0020] Preferably, the stripping liquid includes polyol and phosphoester.|[0021] In the process of crushing the waste lithium iron phosphate battery, with the increasing shearing times, waste and used lithium iron phosphate electrode plates are smaller, and aluminum-copper scraps or aluminum-copper powders in the corresponding electrode material are more, which is not conducive to later removal, resulting in that an aluminum-copper content in the final prepared cathode material is high, which affects the performances of the cathode material. The inventor(s) find(s) that by controlling the sizes of the crushed pieces after shearing and using a stripping liquid containing polyol and phosphoester for stripping treatment, the stripping liquid hardly produced aluminum-copper scraps, which can reduce the aluminum-copper content in the final prepared cathode material and the stripping liquid can be recycled.|[0022] Preferably, the polyol is selected from at least one of ethylene glycol, propylene glycol, propanetriol, isopropanol, butanol, 1,2-butanediol or 1,3-butanediol.|[0023] Preferably, the phosphoester is selected from at least one of phosphomonoester, phosphodiester, phosphotriester, triethyl phosphate or trimethyl phosphate.|[0024] Preferably, a volume ratio of the polyol to the phosphoester is 1:(0.1 to 1); and further preferably, the volume ratio of the polyol to the phosphoester is 1:(0.3 to 0.8).|[0025] Preferably, the primary heating is performed at a temperature of 130° C. to 210° C., and the primary heating lasts for 0.5 hour to 10 hours; and further preferably, the primary heating is performed at a temperature of 160° C. to 210° C., and the primary heating lasts for 1 hour to 8 hours.|[0026] Preferably, the secondary heating is performed at a temperature of 210° C. to 300° C., and the secondary heating lasts for 2 hours to 12 hours.|[0027] Preferably, in step (2), the benzene sulfonate is selected from at least one of sodium p-toluenesulfonate, sodium 4-methylbenzenesulfonate, sodium benzenesulfonate or zinc benzenesulfonate. Benzene sulfonate decomposes at high temperature to produce sulfur dioxide and water, which can promote the pyrolysis of a membrane (polyethylene, polypropylene), an electrolyte (LiClO4, LiPF6, carbonate) and a binder (polyvinylidene fluoride) in the black powder, and is beneficial to remove fluorine and carbon.|[0028] Preferably, in step (2), an addition amount of the benzene sulfonate is 0.1 w % to 5 w % of the black powder; and further preferably, the addition amount of the benzene sulfonate is 0.1 w % to 3 w % of the black powder.|[0029] Preferably, in step (2), the reaction is performed at a temperature of 300° C. to 850° C., and lasts for 1 minute to 360 minutes; and further preferably, in step (2), the reaction is performed at a temperature of 400° C. to 750° C., and lasts for 30 minutes to 240 minutes.|[0030] Preferably, gas in the fluidized bed includes at least one of oxygen, carbon dioxide or nitrogen.|[0031] Preferably, in step (2), a mass percentage of the carbon in the black powder without carbon and fluorine removed is less than 2%.|[0032] In a traditional method, a heating furnace is used to pyrolyze the black powder, and heat released by the heating furnace is transferred from a surface of the black powder to the inside. A part of the heat cannot be transferred into the black powder, which is highly susceptible to cause heat loss, and the inside needs a long heating time, so that the heating furnace cannot fully pyrolyze a diaphragm (polyethylene, polypropylene), an electrolyte (LiClO4, LiPF6, carbonate), a binder (polyvinylidene fluoride) and other substances in the black powder. According to the present disclosure, the fluidized bed pyrolysis method is adopted, and with the use of benzene sulfonate, the black powder layer is heated at a uniform temperature, so that local overheating can be avoided, and the black powder is easy to flow between devices, which has a high conveying capacity, and is suitable for large-scale pyrolysis. The sulfur dioxide and water produced by the benzene sulfonate decomposed at high temperature promotes the pyrolysis of the membrane (polyethylene, polypropylene), the electrolyte (LiClO4, LiPF6, carbonate) and the binder (polyvinylidene fluoride) in the black powder. The combination of the two can make the pyrolysis of fluorine-containing and carbon-containing substances in the black powder more thorough, which is beneficial to the removal of the carbon and fluorine in the black powder.|[0033] Preferably, in step (3), the acid is selected from at least one of phosphoric acid, formic acid, lactic acid, citric acid, oxalic acid or acetic acid.|[0034] Preferably, in step (3), the acid has a molar concentration of 0.01 mol/L to 6 mol/L.|[0035] Preferably, in step (3), the alkali is selected from calcium hydroxide or/and magnesium hydroxide.|[0036] In step (3), the solid A is iron phosphate, the solution A is an impurity-containing lithium hydroxide solution, the solution B is a lithium hydroxide solution, and the solid B is aluminum hydroxide and copper hydroxide.|[0037] Preferably, in step (4), the lithium supplement agent is selected from at least one of lithium carbonate, lithium oxalate or lithium phosphate.|[0038] Preferably, in step (4), the iron supplement agent is selected from at least one of ferric hydroxide, iron phosphate, ferric oxalate, ferrous oxalate, ferric citrate or ferrous citrate.|[0039] Preferably, in step (4), the phosphate is selected from at least one of ammonium phosphate, ammonium hydrogen phosphate, sodium phosphate, ferrous phosphate, iron phosphate or phosphoric acid.|[0040] Preferably, in step (4), a molar ratio of lithium to iron to phosphate radical in the mixture is (0.1 to 20):(0.1 to 20):(0.1 to 20).|[0041] Preferably, in step (4), the reducing agent is selected from at least one of glucose, fructose or starch.|[0042] Preferably, in step (4), an addition amount of the reducing agent accounts for 1 w % to 25 wt % of the mixture.|[0043] Compared with the prior art, the present disclosure has the following beneficial effects.|[0044] (1) The method for recycling and preparing the cathode material from the waste lithium iron phosphate battery proposed by the present disclosure can control and optimize the processes of crushing, stripping, removing carbon and fluorine, and removing impurities to recycle and obtain the cathode material with high purity while controlling the recycling cost, and the batteries prepared again by using the recycled cathode material have good performances.|[0045] (2) The recycling method provided by the present disclosure can not only effectively reduce the contents of aluminum, copper, carbon and fluorine in the black powder, but also only need to supplement iron or lithium for carbothermic reduction when the cathode material is regenerated.|(US12009492)|BRIEF DESCRIPTION OF DRAWINGS|[0046] FIG. 1 is a process flowchart of Embodiment 1;|[0047] FIG. 2 is an SEM graph of a lithium iron phosphate cathode material prepared in Embodiment 1; and|[0048] FIG. 3 is a discharge cycle performance diagram of button batteries assembled with the lithium iron phosphate cathode materials provided in Comparative Example 1 and Embodiment 4.|(US12009492)|DETAILED DESCRIPTION|[0049] In order to make the technical solutions of the present disclosure clearer to those skilled in the art, the following embodiments are listed for explanation. It should be noted that the following embodiments do not limit the scope of protection claimed by the present disclosure.|[0050] Unless otherwise specified, the raw materials, reagents or devices used in the following embodiments can be obtained from conventional commercial sources or by existing known methods.|Embodiment 1|[0051] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery, the process flowchart of which was as shown in FIG. 1, includes the following steps.|[0052] (1) Pre-treating battery: 38.3 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces (electrode plates) to the batteries was about 30%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.5), covered by the stripping liquid, heated up to 170° C. by a heating plant, maintained at the temperature for 2 hours and 20 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously, kept at 225° C. for 3 hours and 30 minutes, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 9.2 kg of black powder.|[0053] (2) Removing carbon and fluorine: 25.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 560° C. Then the black powder was burnt and cooled to recycle 9.17 kg of black powder with carbon and fluorine removed.|[0054] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.6 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0055] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.134:6.063:6.181) was measured, and 0.048 mol of ferrous oxalate and 0.060 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.182:6.181:6.183) were added. Then 90 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 35 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material. FIG. 2 was an SEM graph of the lithium iron phosphate cathode material. In FIG. 2, the regenerated lithium iron phosphate cathode material had a particle size of about 50 nm, and only some particle sizes were about 50 nm to 150 nm. The lithium iron phosphate cathode material had uniform particle size and high concentration of particle size.|Embodiment 2|[0056] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery includes the following steps.|[0057] (1) Pre-treating battery: 23.4 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces to the batteries was about 30%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.5), covered by the stripping liquid, heated up to 160° C. by a heating plant, maintained at the temperature for 2 hours and 20 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously, kept at 215° C. for 4 hours and 25 minutes, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 5.8 kg of black powder.|[0058] (2) Removing carbon and fluorine: 20.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 550° C. Then the black powder was burnt and cooled to recycle 4.6 kg of black powder with carbon and fluorine removed.|[0059] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.6 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0060] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.110:6.037:6.174) was measured, and 0.064 mol of ferrous oxalate and 0.137 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.174:6.174:6.174) were added. Then 85 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 35 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material.|Embodiment 3|[0061] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery includes the following steps.|[0062] (1) Pre-treating battery: 50.2 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces to the batteries was about 30%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.6), covered by the stripping liquid, heated up to 180° C. by a heating plant, maintained at the temperature for 2 hours and 20 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously, kept at 238° C. for 4 hours and 47 minutes, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 11.8 kg of black powder.|[0063] (2) Removing carbon and fluorine: 32.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 570° C. Then the black powder was burnt and cooled to recycle 9.3 kg of black powder with carbon and fluorine removed.|[0064] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.6 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0065] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.142:6.068:6.217) was measured, and 0.067 mol of ferrous oxalate and 0.143 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.209:6.211:6.217) were added. Then 90 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 35 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material.|Embodiment 4|[0066] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery includes the following steps.|[0067] (1) Pre-treating battery: 46.5 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces to the batteries was about 20%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.6), covered by the stripping liquid, heated up to 180° C. by a heating plant, maintained at the temperature for 2 hours and 50 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously, kept at 212° C. for 5 hours and 26 minutes, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 11.3 kg of black powder.|[0068] (2) Removing carbon and fluorine: 32.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 560° C. Then the black powder was burnt and cooled to recycle 8.9 kg of black powder with carbon and fluorine removed.|[0069] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.7 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0070] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.131:6.063:6.196) was measured, and 0.065 mol of ferrous oxalate and 0.134 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.196:6.197:6.196) were added. Then 75 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 31 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material.|Embodiment 5|[0071] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery includes the following steps.|[0072] (1) Pre-treating battery: 42.7 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces to the batteries was about 30%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.6), covered by the stripping liquid, heated up to 180° C. by a heating plant, maintained at the temperature for 2 hours and 40 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously at 244° C. until the separation liquid did not change, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 9.4 kg of black powder.|[0073] (2) Removing carbon and fluorine: 35.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 570° C. Then the black powder was burnt and cooled to recycle 7.4 kg of black powder with carbon and fluorine removed.|[0074] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.7 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0075] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.158:6.104:6.214) was measured, and 0.048 mol of ferrous oxalate and 0.060 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.163:6.161:6.214) were added. Then 80 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 31 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material. (US12009492)|CROSS-REFERENCE TO RELATED APPLICATION|[0001] This application is a national stage filing under 35 U.S.C. § 371 of international application number PCT/CN2022/111816, filed Aug. 11, 2022, which claims priority to Chinese patent application No. 202111367677.5, filed Nov. 18, 2021. The contents of these applications are incorporated herein by reference in their entirety.|(US12009492)|TECHNICAL FIELD|[0002] The present disclosure relates to the technical field of recycling battery materials, and particularly, to a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery.|BACKGROUND|[0003] Although lithium iron phosphate batteries are inferior to those of the same type of transition metal oxide batteries, such as lithium nickel cobalt manganese and lithium manganese, in working voltage platform and capacity density, the lithium iron phosphate batteries are superior to the transition metal oxide batteries in charge and discharge cycle life, safety, thermal stability and manufacturing cost. Therefore, under the demands for long life, low cost and easy use of batteries, the lithium iron phosphate batteries have become a preferred choice for electric energy storage and power batteries. With the development of the lithium iron phosphate battery industry, it can be expected that a large number of waste lithium iron phosphate batteries will be replaced in the future. Therefore, how to deal with and recycle the waste lithium iron phosphate batteries will also become a big problem.|[0004] Currently, recycling the waste lithium iron phosphate batteries generally includes the following steps of: classifying the waste lithium iron phosphate battery according to chemical compositions of the battery, then physically dismounting the waste lithium iron phosphate battery, then performing high-temperature calcination and crushing for separation, and extracting the electrolyte. There are still some problems in this recycling method, for example, during mechanical crushing, waste polyanion batteries may be affected by crushed shells and crushed current collectors and diaphragms, so as to change physical and chemical components of a cathode material to be recycled. On one hand, the crushing process destroys an internal crystal arrangement of the cathode material. On the other hand, the crushing process mixes copper-aluminum and phosphate radical with the electrolyte and the binder together, which increases the difficulty of subsequent purification. Especially, the crushing of aluminum and copper foils makes the aluminum and copper foils be mixed with each other, and the mixture cannot be separated accurately by mechanical separation. Therefore, the recycling cost is high, and the purity of the recycled cathode material is low, and the batteries prepared again cannot meet performance requirements, which also limit the industrial application and popularization of the lithium iron phosphate battery to a certain extent.|[0005] Therefore, it is urgent to provide a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery, which can recycle and obtain a cathode material with high purity while controlling the recycling cost, and batteries prepared again by using the recycled cathode material have good performances.|SUMMARY|[0006] The present disclosure aims at solving at least one of the above-mentioned technical problems in the prior art. Therefore, the present disclosure proposes a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery, which can recycle and obtain a cathode material with high purity while controlling the recycling cost, and batteries prepared again by using the recycled cathode material have good performances.|[0007] The present disclosure provides a method for recycling and preparing a cathode material from a waste lithium iron phosphate battery.|[0008] Specifically, the method for recycling and preparing the cathode material from the waste lithium iron phosphate battery includes the following steps of:| - (1) discharging a waste lithium iron phosphate battery, drying an electrolyte inside the waste lithium iron phosphate battery, then crushing to obtain crushed pieces, and stripping the crushed pieces to obtain a black powder;| - (2) mixing the black powder obtained in step (1) with benzene sulfonate, and then reacting in a fluidized bed to obtain a black powder without carbon and fluorine removed;| - (3) adding acid into the black powder without carbon and fluorine removed in step (2) for solid-liquid separation to obtain a solution A and a solid A; and then, adding alkali into the solution A until no precipitation is generated, and performing solid-liquid separation to obtain a solution B and a solid B; and| - (4) mixing the solid A and the solution B obtained in step (3), adding at least one of a lithium supplement agent, an iron supplement agent or phosphate to obtain a mixture, then adding a reducing agent into the mixture, and sintering to obtain a cathode material.|[0013] Preferably, in step (1), the discharging process is that the waste lithium iron phosphate battery is placed in a solution of metal salt and discharged for 0.1 day to 10 days.|[0014] Preferably, the metal salt is selected from one or more of sodium chloride, sodium sulfate, sodium phosphate, magnesium chloride, magnesium sulfate, lithium sulfate or lithium chloride.|[0015] Preferably, in the solution of the metal salt, a mass concentration of the metal salt respectively ranges from 0.1 w % to 20 w %.|[0016] Preferably, in step (1), the drying process is that the waste lithium iron phosphate battery is placed in a sintering furnace, a kiln, a muffle furnace, an electric furnace or an oven and dried at 15° C. to 150° C. for 1 hour to 120 hours. Alternatively, the waste lithium iron phosphate battery may be placed under solar radiation.|[0017] Preferably, in step (1), the crushing process is that the waste lithium iron phosphate battery is sheared for 1 times to 10 times to obtain the crushed pieces.|[0018] Preferably, an area ratio of the crushed pieces to the waste lithium iron phosphate battery is greater than 5%; and further preferably, the area ratio of the crushed pieces to the waste lithium iron phosphate battery is greater than 10%.|[0019] Preferably, in step (1), the stripping process is that the crushed pieces are placed in a stripping liquid, subjected to primary heating, and separated into a solid and a separated liquid; and then, the separated liquid is subjected to secondary heating, and the stripping liquid is removed to obtain the black powder. The solid refers to aluminum and copper foils which are recycled after separation.|[0020] Preferably, the stripping liquid includes polyol and phosphoester.|[0021] In the process of crushing the waste lithium iron phosphate battery, with the increasing shearing times, waste and used lithium iron phosphate electrode plates are smaller, and aluminum-copper scraps or aluminum-copper powders in the corresponding electrode material are more, which is not conducive to later removal, resulting in that an aluminum-copper content in the final prepared cathode material is high, which affects the performances of the cathode material. The inventor(s) find(s) that by controlling the sizes of the crushed pieces after shearing and using a stripping liquid containing polyol and phosphoester for stripping treatment, the stripping liquid hardly produced aluminum-copper scraps, which can reduce the aluminum-copper content in the final prepared cathode material and the stripping liquid can be recycled.|[0022] Preferably, the polyol is selected from at least one of ethylene glycol, propylene glycol, propanetriol, isopropanol, butanol, 1,2-butanediol or 1,3-butanediol.|[0023] Preferably, the phosphoester is selected from at least one of phosphomonoester, phosphodiester, phosphotriester, triethyl phosphate or trimethyl phosphate.|[0024] Preferably, a volume ratio of the polyol to the phosphoester is 1:(0.1 to 1); and further preferably, the volume ratio of the polyol to the phosphoester is 1:(0.3 to 0.8).|[0025] Preferably, the primary heating is performed at a temperature of 130° C. to 210° C., and the primary heating lasts for 0.5 hour to 10 hours; and further preferably, the primary heating is performed at a temperature of 160° C. to 210° C., and the primary heating lasts for 1 hour to 8 hours.|[0026] Preferably, the secondary heating is performed at a temperature of 210° C. to 300° C., and the secondary heating lasts for 2 hours to 12 hours.|[0027] Preferably, in step (2), the benzene sulfonate is selected from at least one of sodium p-toluenesulfonate, sodium 4-methylbenzenesulfonate, sodium benzenesulfonate or zinc benzenesulfonate. Benzene sulfonate decomposes at high temperature to produce sulfur dioxide and water, which can promote the pyrolysis of a membrane (polyethylene, polypropylene), an electrolyte (LiClO4, LiPF6, carbonate) and a binder (polyvinylidene fluoride) in the black powder, and is beneficial to remove fluorine and carbon.|[0028] Preferably, in step (2), an addition amount of the benzene sulfonate is 0.1 w % to 5 w % of the black powder; and further preferably, the addition amount of the benzene sulfonate is 0.1 w % to 3 w % of the black powder.|[0029] Preferably, in step (2), the reaction is performed at a temperature of 300° C. to 850° C., and lasts for 1 minute to 360 minutes; and further preferably, in step (2), the reaction is performed at a temperature of 400° C. to 750° C., and lasts for 30 minutes to 240 minutes.|[0030] Preferably, gas in the fluidized bed includes at least one of oxygen, carbon dioxide or nitrogen.|[0031] Preferably, in step (2), a mass percentage of the carbon in the black powder without carbon and fluorine removed is less than 2%.|[0032] In a traditional method, a heating furnace is used to pyrolyze the black powder, and heat released by the heating furnace is transferred from a surface of the black powder to the inside. A part of the heat cannot be transferred into the black powder, which is highly susceptible to cause heat loss, and the inside needs a long heating time, so that the heating furnace cannot fully pyrolyze a diaphragm (polyethylene, polypropylene), an electrolyte (LiClO4, LiPF6, carbonate), a binder (polyvinylidene fluoride) and other substances in the black powder. According to the present disclosure, the fluidized bed pyrolysis method is adopted, and with the use of benzene sulfonate, the black powder layer is heated at a uniform temperature, so that local overheating can be avoided, and the black powder is easy to flow between devices, which has a high conveying capacity, and is suitable for large-scale pyrolysis. The sulfur dioxide and water produced by the benzene sulfonate decomposed at high temperature promotes the pyrolysis of the membrane (polyethylene, polypropylene), the electrolyte (LiClO4, LiPF6, carbonate) and the binder (polyvinylidene fluoride) in the black powder. The combination of the two can make the pyrolysis of fluorine-containing and carbon-containing substances in the black powder more thorough, which is beneficial to the removal of the carbon and fluorine in the black powder.|[0033] Preferably, in step (3), the acid is selected from at least one of phosphoric acid, formic acid, lactic acid, citric acid, oxalic acid or acetic acid.|[0034] Preferably, in step (3), the acid has a molar concentration of 0.01 mol/L to 6 mol/L.|[0035] Preferably, in step (3), the alkali is selected from calcium hydroxide or/and magnesium hydroxide.|[0036] In step (3), the solid A is iron phosphate, the solution A is an impurity-containing lithium hydroxide solution, the solution B is a lithium hydroxide solution, and the solid B is aluminum hydroxide and copper hydroxide.|[0037] Preferably, in step (4), the lithium supplement agent is selected from at least one of lithium carbonate, lithium oxalate or lithium phosphate.|[0038] Preferably, in step (4), the iron supplement agent is selected from at least one of ferric hydroxide, iron phosphate, ferric oxalate, ferrous oxalate, ferric citrate or ferrous citrate.|[0039] Preferably, in step (4), the phosphate is selected from at least one of ammonium phosphate, ammonium hydrogen phosphate, sodium phosphate, ferrous phosphate, iron phosphate or phosphoric acid.|[0040] Preferably, in step (4), a molar ratio of lithium to iron to phosphate radical in the mixture is (0.1 to 20):(0.1 to 20):(0.1 to 20).|[0041] Preferably, in step (4), the reducing agent is selected from at least one of glucose, fructose or starch.|[0042] Preferably, in step (4), an addition amount of the reducing agent accounts for 1 w % to 25 wt % of the mixture.|[0043] Compared with the prior art, the present disclosure has the following beneficial effects.|[0044] (1) The method for recycling and preparing the cathode material from the waste lithium iron phosphate battery proposed by the present disclosure can control and optimize the processes of crushing, stripping, removing carbon and fluorine, and removing impurities to recycle and obtain the cathode material with high purity while controlling the recycling cost, and the batteries prepared again by using the recycled cathode material have good performances.|[0045] (2) The recycling method provided by the present disclosure can not only effectively reduce the contents of aluminum, copper, carbon and fluorine in the black powder, but also only need to supplement iron or lithium for carbothermic reduction when the cathode material is regenerated.|(US12009492)|BRIEF DESCRIPTION OF DRAWINGS|[0046] FIG. 1 is a process flowchart of Embodiment 1;|[0047] FIG. 2 is an SEM graph of a lithium iron phosphate cathode material prepared in Embodiment 1; and|[0048] FIG. 3 is a discharge cycle performance diagram of button batteries assembled with the lithium iron phosphate cathode materials provided in Comparative Example 1 and Embodiment 4.|(US12009492)|DETAILED DESCRIPTION|[0049] In order to make the technical solutions of the present disclosure clearer to those skilled in the art, the following embodiments are listed for explanation. It should be noted that the following embodiments do not limit the scope of protection claimed by the present disclosure.|[0050] Unless otherwise specified, the raw materials, reagents or devices used in the following embodiments can be obtained from conventional commercial sources or by existing known methods.|Embodiment 1|[0051] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery, the process flowchart of which was as shown in FIG. 1, includes the following steps.|[0052] (1) Pre-treating battery: 38.3 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces (electrode plates) to the batteries was about 30%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.5), covered by the stripping liquid, heated up to 170° C. by a heating plant, maintained at the temperature for 2 hours and 20 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously, kept at 225° C. for 3 hours and 30 minutes, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 9.2 kg of black powder.|[0053] (2) Removing carbon and fluorine: 25.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 560° C. Then the black powder was burnt and cooled to recycle 9.17 kg of black powder with carbon and fluorine removed.|[0054] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.6 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0055] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.134:6.063:6.181) was measured, and 0.048 mol of ferrous oxalate and 0.060 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.182:6.181:6.183) were added. Then 90 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 35 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material. FIG. 2 was an SEM graph of the lithium iron phosphate cathode material. In FIG. 2, the regenerated lithium iron phosphate cathode material had a particle size of about 50 nm, and only some particle sizes were about 50 nm to 150 nm. The lithium iron phosphate cathode material had uniform particle size and high concentration of particle size.|Embodiment 2|[0056] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery includes the following steps.|[0057] (1) Pre-treating battery: 23.4 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces to the batteries was about 30%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.5), covered by the stripping liquid, heated up to 160° C. by a heating plant, maintained at the temperature for 2 hours and 20 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously, kept at 215° C. for 4 hours and 25 minutes, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 5.8 kg of black powder.|[0058] (2) Removing carbon and fluorine: 20.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 550° C. Then the black powder was burnt and cooled to recycle 4.6 kg of black powder with carbon and fluorine removed.|[0059] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.6 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0060] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.110:6.037:6.174) was measured, and 0.064 mol of ferrous oxalate and 0.137 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.174:6.174:6.174) were added. Then 85 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 35 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material.|Embodiment 3|[0061] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery includes the following steps.|[0062] (1) Pre-treating battery: 50.2 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces to the batteries was about 30%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.6), covered by the stripping liquid, heated up to 180° C. by a heating plant, maintained at the temperature for 2 hours and 20 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously, kept at 238° C. for 4 hours and 47 minutes, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 11.8 kg of black powder.|[0063] (2) Removing carbon and fluorine: 32.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 570° C. Then the black powder was burnt and cooled to recycle 9.3 kg of black powder with carbon and fluorine removed.|[0064] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.6 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0065] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.142:6.068:6.217) was measured, and 0.067 mol of ferrous oxalate and 0.143 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.209:6.211:6.217) were added. Then 90 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 35 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material.|Embodiment 4|[0066] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery includes the following steps.|[0067] (1) Pre-treating battery: 46.5 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces to the batteries was about 20%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.6), covered by the stripping liquid, heated up to 180° C. by a heating plant, maintained at the temperature for 2 hours and 50 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously, kept at 212° C. for 5 hours and 26 minutes, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 11.3 kg of black powder.|[0068] (2) Removing carbon and fluorine: 32.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 560° C. Then the black powder was burnt and cooled to recycle 8.9 kg of black powder with carbon and fluorine removed.|[0069] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.7 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0070] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.131:6.063:6.196) was measured, and 0.065 mol of ferrous oxalate and 0.134 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.196:6.197:6.196) were added. Then 75 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 31 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material.|Embodiment 5|[0071] A method for recycling and preparing a cathode material from a waste lithium iron phosphate battery includes the following steps.|[0072] (1) Pre-treating battery: 42.7 kg of recycled waste lithium iron phosphate batteries were put into tap water containing 1.7% sodium chloride (mass concentration), discharged for 4 days, and then exposed to solar radiation to dry electrolytes inside the batteries. The batteries were sheared for three times to get crushed pieces, and make an area ratio of the crushed pieces to the batteries was about 30%. The crushed pieces were placed in a stripping liquid (a volume ratio of propanetriol to triethyl phosphate was 1:0.6), covered by the stripping liquid, heated up to 180° C. by a heating plant, maintained at the temperature for 2 hours and 40 minutes, stirred and sieved to obtain solids and a separation liquid. The solids were aluminum and copper foils and recycled. The separation liquid containing plate-like active substances was heated continuously at 244° C. until the separation liquid did not change, and the stripping liquid was recycled to separate the plate-like active substances. The plate-like active substances were ground and demagnetized to obtain 9.4 kg of black powder.|[0073] (2) Removing carbon and fluorine: 35.0 g of sodium p-toluenesulfonate were added into the black powder obtained in step (1) and mixed. A heater and a pump of a fluidized bed were enabled to heat and pump air, and pump the black powder to a combustion chamber for reaction. A heating temperature of the combustion was controlled to be about 570° C. Then the black powder was burnt and cooled to recycle 7.4 kg of black powder with carbon and fluorine removed.|[0074] (3) Removing impurities: 1.0 kg of black powder with carbon and fluorine removed were taken and pickled with 1 mol/L phosphoric acid for solid-liquid separation to obtain a solid A and a solution A. The solid A was washed with water for later use. 2.7 g of calcium hydroxide were added to the solution A and stirred to adjust a pH until the precipitation did not increase, and then solid-liquid separation was performed to obtain a solid B and a solution B. The solution B was a solution containing lithium hydroxide.|[0075] (4) Regenerating cathode material: The solid A and the solution B were mixed and evaporated to remove water. A molar ratio of iron to lithium and phosphate in the evaporated solid (mol=6.158:6.104:6.214) was measured, and 0.048 mol of ferrous oxalate and 0.060 mol of lithium carbonate (molar ratio of iron to lithium and phosphate radical=6.163:6.161:6.214) were added. Then 80 g of glucose were added for mixing and ball-milling, heated to 570° C. in neon environment, sintered for 8 hours and 31 minutes, and cooled to obtain regenerated lithium iron phosphate cathode material.|(US12009492)|Comparative Example 1|[0076] Comparative Example 1 was different from Embodiment 1 in that: In the treatment of removing carbon and fluorine in step (2), conventional heating pipes were used for removing carbon and fluorine. The black powder was sent to a tube furnace and heated at 510° C. for 8 hours to remove carbon and fluorine. The remaining steps were the same as that in Embodiment 1.|Comparative Example 2|[0077] Comparative Example 2 was different from Embodiment 1 in that: no sodium p-toluenesulfonate was added in step (2), and only the fluidized bed was used for removing carbon and fluorine. The remaining steps were the same as that in Embodiment 1.|[0078] Product Effect Test:|[0079] (1) Contents of the carbon and the fluorine in the black powder before and after removing carbon and fluorine in each embodiment and comparative example were tested. The test results were shown in Table 1.|[0080] TABLE 1 Contents of carbon and fluorine in black powderbefore and after removing carbon and fluorinein embodiments and comparative examples CarbonFluorineEmbodimentcontent (%)content (%) Embodiment 1Before removing20.320.016 carbon and fluorine After removing1.780.0038 carbon and fluorineEmbodiment 2Before removing20.360.019 carbon and fluorine After removing1.870.0041 carbon and fluorineEmbodiment 3Before removing20.330.016 carbon and fluorine After removing1.390.0028 carbon and fluorineEmbodiment 4Before removing20.260.018 carbon and fluorine After removing1.640.0017 carbon and fluorineEmbodiment 5Before removing20.190.015 carbon and fluorine After removing1.450.0023 carbon and fluorineComparativeBefore removing20.380.015Example 1carbon and fluorine After removing3.450.0087 carbon and fluorineComparativeBefore removing20.290.016Example 2carbon and fluorine After removing2.590.0050 carbon and fluorine |[0081] From Table 1, it can be seen that the carbon and fluorine contents of the black powder after removing carbon and fluorine in the embodiments are obviously lower than those of the comparative examples, and the carbon and fluorine can be effectively removed by using the fluidized bed combined with the benzene sulfonate for removing carbon and fluorine.|[0082] (2) The lithium iron phosphate cathode materials prepared in Embodiments 1 to 5 and Comparative Examples 1 to 2 were taken respectively to assemble button batteries. The specific assembly process was as follows.|[0083] The lithium phosphate cathode material, acetylene black and polyvinylidene fluoride (PVDF) were weighed according to a mass ratio of 8:1:1, mixed, stirred and ground, and a certain amount N-methyl pyrrolidone (NMP) solution was added as a solvent, and a slurry was obtained after stirring the mixture. The slurry was evenly coated on a clean aluminum foil, then placed in a heating pipe at 70° C. for 6 hours, and stamped into electrode plates with a diameter of about 15 mm. The lithium ion button battery was assembled in a glove box filled with neon gas. The prepared electrode plate was used as a cathode and 1.0 mol/LiPF6 (solvent being vinyl carbonate) was used as an electrolyte. The button battery was assembled according to the order of a shell, an elastic sheet, a gasket, an anode (lithium metal plate), 0.25 mL of electrolyte, a diaphragm (polypropylene film), a cathode (electrode plate) and a shell.|[0084] Then, charge and discharge performances of the assembled batteries were tested on a constant current charge and discharge test device. The test conditions were as follows: a voltage range was 2.0 V to 3.5 V, a test rate was 0.5 C (152 mAh·g−1), and the results of 30 cycles at 0.5 C rate were shown in Table 2.|[0085]  TABLE 2    The first timeThe 30th times Group(mAh · g−1)(mAh · g−1)    Embodiment 1156.4155.6 Embodiment 2156.8155.6 Embodiment 3156.7156.1 Embodiment 4156.9155.7 Embodiment 5156.5155.7 Comparative Example 1156.2154.3 Comparative Example 2155.8154.6  |[0086] It can be known from Table 2 that the button batteries assembled with the lithium iron phosphate cathode materials provided by the embodiments have a specific capacity of 156 mAh·g−1 or more after 30 cycles, and have excellent electrical performances which are obviously superior to these of the comparative examples. FIG. 3 is a discharge cycle performance diagram of the button batteries assembled with the lithium iron phosphate cathode materials provided in Comparative Example 1 and Embodiment 4. In FIG. 3, the X-coordinate refers to a cycle index, and the Y-coordinate refers to a discharge capacity. The 30-times discharge capacity of the button battery of Comparative Example 1 ranges from 154.3 mAh·g−1 to 156.2 mAh·g−1, and the 30-times discharge capacity of the button battery of Embodiment 4 ranges from 155.6 mAh·g−1 to 156.4 mAh·g−1. The lithium iron phosphate cathode material provided by Embodiment 4 has better cycle stability. Family Number|(99304691)|99304691|Abstract|(CN114229816B B)|The invention belongs to the technical field of battery material recovery , and discloses a method for recovering and preparing a positive electrode material from a waste lithium iron phosphate battery . The method comprises the following steps : discharging , crushing and stripping the waste lithium iron phosphate battery to obtain black powder ; mixing the black powder with benzene sulfonate , and reacting in a fluidized bed ; and adding acid and alkali to remove impurities , finally adding a lithium supplement agent , an iron supplement agent or phosphate and a reducing agent , and sintering . According to the method , the processes of crushing , stripping , decarburization and defluorination and impurity removal are controlled and optimized , so that the high - purity positive electrode material can be recycled while the recycling cost is controlled , and the battery prepared by utilizing the recycled positive electrode material again has good performance . According to the method , the content of aluminum , copper , carbon and fluorine in the black powder can be effectively reduced , and when the positive electrode material is regenerated , only iron or lithium needs to be supplemented , and carbon thermal reduction is carried out . |(WO202387800 A1)|A method for recycling and preparing a positive electrode material from waste lithium iron phosphate batteries. The method comprises the following steps: discharging, crushing, and stripping waste lithium iron phosphate batteries to obtain black powder; then mixing the black powder with benzenesulfonate, and reacting in a fluidized bed; and then adding an acid and an alkali to remove impurities, finally adding a lithium supplement, an iron supplement, or a phosphate, and a reducing agent, and sintering. According to the method, by controlling and optimizing the crushing, stripping, carbon and fluorine removal, and impurity removal processes, a positive electrode material with high purity can be recycled while controlling the recycling cost, and batteries prepared by means of the recycled positive electrode material have good performance. According to the method, the contents of aluminum, copper, carbon, and fluorine in the black powder can be effectively reduced; moreover, when regenerating a positive electrode material, there is only a need to supplement iron or lithium and carry out carbothermic reduction.|(DE112022000199 B4)|Process for recycling and producing a positive electrode material from waste lithium iron phosphate batteries. The method comprises the following steps: discharging, comminuting and stripping used lithium iron phosphate batteries in order to obtain black powder; then mixing the black powder with benzene sulfonate and reacting in a fluidized bed; and then adding an acid and an alkali in order to remove impurities, finally adding a lithium additive, an iron additive or a phosphate and a reducing agent and sintering. By controlling and optimizing the processes of comminution, stripping, carbon and fluorine removal and impurity removal, a positive electrode material can be recycled with high purity while simultaneously controlling the recycling costs, and the batteries produced with the recycled positive electrode material have good performance. With this process, the content of aluminum, copper, carbon and fluorine in the black powder can be effectively reduced; in addition, in the regeneration of a positive electrode material, only iron or lithium has to be added and a carbothermal reduction carried out.|(GB2620690 B)|A method for recycling and preparing a positive electrode material from waste lithium iron phosphate batteries. The method comprises the following steps: discharging, crushing, and stripping waste lithium iron phosphate batteries to obtain black powder; then mixing the black powder with benzenesulfonate, and reacting in a fluidized bed; and then adding an acid and an alkali to remove impurities, finally adding a lithium supplement, an iron supplement, or a phosphate, and a reducing agent, and sintering. According to the method, by controlling and optimizing the crushing, stripping, carbon and fluorine removal, and impurity removal processes, a positive electrode material with high purity can be recycled while controlling the recycling cost, and batteries prepared by means of the recycled positive electrode material have good performance. According to the method, the contents of aluminum, copper, carbon, and fluorine in the black powder can be effectively reduced; moreover, when regenerating a positive electrode material, there is only a need to supplement iron or lithium and carry out carbothermic reduction.|(US12009492 B2)|A method for recycling and preparing a positive electrode material from waste lithium iron phosphate batteries. The method comprises the following steps: discharging, crushing, and stripping waste lithium iron phosphate batteries to obtain black powder; then mixing the black powder with benzenesulfonate, and reacting in a fluidized bed; and then adding an acid and an alkali to remove impurities, finally adding a lithium supplement, an iron supplement, or a phosphate, and a reducing agent, and sintering. According to the method, by controlling and optimizing the crushing, stripping, carbon and fluorine removal, and impurity removal processes, a positive electrode material with high purity can be recycled while controlling the recycling cost, and batteries prepared by means of the recycled positive electrode material have good performance.|(ES2963369 R1)|A method for recycling and preparing a positive electrode material from waste lithium iron phosphate batteries. The method comprises the following steps: discharging, crushing, and stripping waste lithium iron phosphate batteries to obtain black powder; then mixing the black powder with benzenesulfonate, and reacting in a fluidized bed; and then adding an acid and an alkali to remove impurities, finally adding a lithium supplement, an iron supplement, or a phosphate, and a reducing agent, and sintering. According to the method, by controlling and optimizing the crushing, stripping, carbon and fluorine removal, and impurity removal processes, a positive electrode material with high purity can be recycled while controlling the recycling cost, and batteries prepared by means of the recycled positive electrode material have good performance. According to the method, the contents of aluminum, copper, carbon, and fluorine in the black powder can be effectively reduced; moreover, when regenerating a positive electrode material, there is only a need to supplement iron or lithium and carry out carbothermic reduction.|(MX-415021 B)|A method for recycling and preparing a positive electrode material from waste lithium iron phosphate batteries. The method comprises the following steps: discharging, crushing, and stripping waste lithium iron phosphate batteries to obtain black powder; then mixing the black powder with benzenesulfonate, and reacting in a fluidized bed; and then adding an acid and an alkali to remove impurities, finally adding a lithium supplement, an iron supplement, or a phosphate, and a reducing agent, and sintering. According to the method, by controlling and optimizing the crushing, stripping, carbon and fluorine removal, and impurity removal processes, a positive electrode material with high purity can be recycled while controlling the recycling cost, and batteries prepared by means of the recycled positive electrode material have good performance. According to the method, the contents of aluminum, copper, carbon, and fluorine in the black powder can be effectively reduced; moreover, when regenerating a positive electrode material, there is only a need to supplement iron or lithium and carry out carbothermic reduction.|CPC codes|(CN114229816B B)|C01B - 025/45 |C01P - 2004/03 |C01P - 2004/64 |C01P - 2006/40 |(WO202387800 A1)|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|(DE112022000199 B4)|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|(GB2620690 B)|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|(US12009492 B2)|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|(HU-231541 B1)|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|(ES2963369 R1)|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|(MX-415021 B)|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|IPC codes|(CN114229816B B)|C01B - 025/45 |(WO202387800 A1)|C01B-025/45|(GB2620690 B)|C01B-025/45|(US12009492 B2)|C01B-025/45|(HU-231541 B1)|C01B-025/45|(ES2963369 R1)|C01B-025/45|(MX-415021 B)|C01B-025/45| Electrical machinery, apparatus, energy|Environmental technology|Materials, metallurgy|Micro-structure and nano-technology B09B-003/70|B82Y-030/00|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|H01M-004/1397|H01M-004/58/25|H01M-010/0525|H01M-010/54|H01M-2004/028|Y02W-030/84 B09B-003/70|B82Y-030/00|C01B-025/45|C01P-2004/03|C01P-2004/64|C01P-2006/40|H01M-004/1397|H01M-004/58/25|H01M-010/0525|H01M-010/54|H01M-2004/028|Y02W-030/84 B09B-003/70|B82Y-030/00|C01B-025/45|H01M-004/02|H01M-004/1391|H01M-004/58|H01M-010/0525|H01M-010/54 B09B-003/70|B82Y-030/00|C01B-025/45|H01M-004/02|H01M-004/1391|H01M-004/1397|H01M-004/58|H01M-010/0525|H01M-010/54 CN118145614|WO202387800|CN120970250|CN119833806|CN118880062|CN118676462|CN116902953|CN116683082B|WO2024130856|CN115602958|CN115072751B|US12494523|US12431553|US12456768|CN118017064B|GB2620690;GB2620690;GB2620690|US12009492 CN118145614 110107332 WHO=Examiner SELF=N CAT=Y|WO202387800 99304691 WHO=Examiner SELF=Y CAT=P CAT=X|CN120970250 116687372 WHO=Examiner SELF=N CAT=A|CN119833806 114221734 WHO=Examiner SELF=N CAT=A|CN118880062 112023782 WHO=Examiner SELF=N CAT=A|CN118676462 111523189 WHO=Examiner SELF=N CAT=A|CN116902953 106946465 WHO=Examiner SELF=N CAT=A|CN116683082B 106351572 WHO=Examiner SELF=N CAT=A|WO2024130856 104202556 WHO=Examiner SELF=Y CAT=A|CN115602958 103440983 WHO=Examiner SELF=N CAT=A|CN115072751B 101832000 WHO=Examiner SELF=N CAT=A|US12494523 112691118 WHO=Applicant SELF=N|US12431553 107190928 WHO=Applicant SELF=N|US12456768 107190928 WHO=Examiner SELF=N|CN118017064B 109732552 WHO=Examiner SELF=N|GB2620690 99304691 WHO=Examiner SELF=Y|US12009492 99304691 WHO=Applicant SELF=Y CN114229816|CN113151682|CN113151682|CN111945016|CN111924819|KR20210085420|CA3076688|CN110649342|CN102208706|CN102208706|US8404138|JP2000348782|CN114229816|CN114229816|CN113151682|CN113151682|CN113151682|CN112811404|CN112320780|CN111945016|CN111945016|CN111924819|CN111924819|KR20210085420|KR20210085420|WO2020134773|WO2017215283|WO2017215283|CN102709620|CN102709620|CN102208706|CN102208706|CN102208706|US20100012149|JP2000348782|JP2000348782 CN114229816 99304691 WHO=Examiner SELF=Y CAT=P CAT=X|CN113151682 95346046 WHO=Examiner SELF=N CAT=A|CN113151682 95346046 WHO=Examiner SELF=N CAT=A|CN111945016 91512286 WHO=Examiner SELF=N CAT=A|CN111924819 91463333 WHO=Examiner SELF=N CAT=A|KR20210085420 95097199 WHO=Examiner SELF=N CAT=A|CA3076688 84031029 WHO=Examiner SELF=N CAT=A|CN110649342 87184728 WHO=Examiner SELF=N CAT=A|CN102208706 7449437 WHO=Examiner SELF=N CAT=A|CN102208706 7449437 WHO=Examiner SELF=N CAT=A|US8404138 4156402 WHO=Examiner SELF=N CAT=A|JP2000348782 22584189 WHO=Examiner SELF=N CAT=A|CN114229816 99304691 WHO=Applicant SELF=Y|CN114229816 99304691 WHO=Examiner SELF=Y|CN113151682 95346046 WHO=Applicant SELF=N|CN113151682 95346046 WHO=Examiner SELF=N|CN113151682 95346046 WHO=Applicant SELF=N|CN112811404 94090602 WHO=Examiner SELF=N|CN112320780 92612638 WHO=Applicant SELF=N|CN111945016 91512286 WHO=Applicant SELF=N|CN111945016 91512286 WHO=Examiner SELF=N|CN111924819 91463333 WHO=Applicant SELF=N|CN111924819 91463333 WHO=Examiner SELF=N|KR20210085420 95097199 WHO=Applicant SELF=N|KR20210085420 95097199 WHO=Examiner SELF=N|WO2020134773 84380504 WHO=Applicant SELF=N|WO2017215283 74167363 WHO=Applicant SELF=N|WO2017215283 74167363 WHO=Examiner SELF=N|CN102709620 7867036 WHO=Applicant SELF=N|CN102709620 7867036 WHO=Examiner SELF=N|CN102208706 7449437 WHO=Applicant SELF=N|CN102208706 7449437 WHO=Examiner SELF=N|CN102208706 7449437 WHO=Applicant SELF=N|US20100012149 4156402 WHO=Examiner SELF=N|JP2000348782 22584189 WHO=Applicant SELF=N|JP2000348782 22584189 WHO=Examiner SELF=N CN114229816; CN102208706; CN111945016; CN113151682; KR20210085420; JP2000348782|CN102208706; US8404138; CA3076688; CN111924819; CN110649342; CN113151682|CN112320780; WO2020134773; CN113151682; CN102208706||US20100012149; CN112811404; CN102208706; CN102709620; CN111924819; CN111945016; CN113151682; CN114229816; JP2000348782; KR20210085420; WO2017215283|CN114229816; CN113151682; CN111945016; CN102208706; JP2000348782; KR20210085420|||CN111924819; CN102709620; WO2017215283 (US12009492)|Search Report references [Examiner]|-Yadav, Prasad, et al. “Recycling of cathode from spent lithium iron phosphate batteries.” Journal of Hazardous Materials, vol. 399, May 30, 2020, p. 123068, https://doi.org/10.1016/j.jhazmat.2020.123068. (Year: 2020).|-Notification to Grant Patent Right for Invention in Chinese patent application No. 202111367677.5 mailed Jan. 11, 2023.|-International Search Report for PCT/CN2022/111816 mailed Oct. 26, 2022.|-Written Opinion for PCT/CN2022/111816 mailed Oct. 26, 2022.|-First Search in Chinese Patent Application 2021113676775 mailed Nov. 25, 2022.|||||||| GRANTED (US12009492)|GRANTED|(WO2023/087800)|LAPSED|(GB2620690)|GRANTED|(DE112022000199)|GRANTED|(CN114229816)|GRANTED|(HU231541)|GRANTED|(MX415021)|GRANTED|(ES2963369)|PENDING ALIVE (US12009492)|ALIVE|(WO2023/087800)|DEAD|(GB2620690)|ALIVE|(DE112022000199)|ALIVE|(CN114229816)|ALIVE|(HU231541)|ALIVE|(MX415021)|ALIVE|(ES2963369)|ALIVE (US12009492)|LEGAL DETAILS FOR US12009492|Actual or expected expiration date=2042-08-11|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-08-11|Event code=US/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=US US18260005|Application 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MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (US12009492)|US|(WO2023/087800)|DE; ES; GB; HU; MX; US|(GB2620690)|GB|(DE112022000199)|DE|(CN114229816)|CN|(HU231541)|HU|(MX415021)|MX|(ES2963369)|ES https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=WYeGGh5krJFVDvm9KHMIpbaa7teVYIYQWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022000499&ekey=1994&xpn=US12009492&kind=B2 https://data.uspto.gov/patent-file-wrapper/search/details/18260005/application-data https://permalink.orbit.com/RenderStaticFirstPage?XPN=U1cupNZCidBsKFytKYx2RTNfFPLuVTJ9KaVWfLIclG0%3D%26n%3D1&id=0&base=FAMPAT CN (WO2023/087800)|CN|(CN114229816)|CN|(CN114229816)|CN (WO2023/087800)|NAME=GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. No. 6 Zhixin Avenue, Leping Town, Sanshui District Foshan, Guangdong 528137 , COUNTRY=CN NAME=HUNAN BRUNP RECYCLING TECHNOLOGY CO., LTD. No. 508 East Jinning Road, Hi-Tech Zone, Ningxiang Changsha, Hunan 410600 , COUNTRY=CN NAME=YICHANG BRUNP CONTEMPORARY AMPEREX CO., LTD. Room 6213 Innovation and Entrepreneurship Service Center, Development Avenue No. 57-5, Yichang Zone, China (Hubei) Free Trade Zone Yichang, Hubei 443000 , COUNTRY=CN|(CN114229816)|NAME=GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. , COUNTRY=CN|(CN114229816)|NAME=GUANGDONG BRUNP RECYCLING TECHNOLOGY CO., LTD. , COUNTRY=CN |(WO2023/087800)|CN|(DE112022000199)|DE|(DE112022000199)|DE||| (US12009492)|NAME=Buchalter NAME=Croft Jason W.|(WO2023/087800)|NAME=JIAQUAN IP LAW No. 910, Building A Winner Plaza, No. 100, West Huangpu Avenue, Tianhe District Guangzhou, Guangdong 510627 , POSTCODE=510627 , COUNTRY=CN|(DE112022000199)|NAME=Spies & Behrndt Patentanwälte PartG mbB , CITY=München , POSTCODE=80687 , COUNTRY=DE|(DE112022000199)|NAME=Spies & Behrndt Patentanwälte PartG mbB , CITY=München , POSTCODE=80687 , COUNTRY=DE|(CN114229816)|NAME=HUANG FEIFEI;JIAQUAN IP LAW , REG=44205|(CN114229816)|NAME=HUANG FEIFEI;JIAQUAN IP LAW , REG=44205|(MX415021)|NAME=LUISA IRELY AQUIQUE PINEDA (US12009492)|CN; CN; CN; CN; CN; CN|(US20240063451)|CN; CN; CN; CN; CN; CN|(WO2023/087800)|CN; CN; CN; CN; CN; CN||||(DE112022000199)|CN; CN; CN; CN; CN; CN|(DE112022000199)|CN; CN; CN; CN; CN; CN|||||(MX415021)|CN; CN; CN; CN; CN; CN||| (US12009492)|NAME=Yu Haijun, CITY=Foshan, COUNTRY=CN |NAME=Li Aixia, CITY=Foshan, COUNTRY=CN |NAME=Xie Yinghao, CITY=Foshan, COUNTRY=CN |NAME=Li Changdong, CITY=Foshan, COUNTRY=CN |NAME=Zhang Xuemei, CITY=Foshan, COUNTRY=CN |NAME=Zhong Yingsheng, CITY=Foshan, COUNTRY=CN|(US20240063451)|NAME=YU Haijun, CITY=Foshan, COUNTRY=CN |NAME=LI Aixia, CITY=Foshan, COUNTRY=CN |NAME=XIE Yinghao, CITY=Foshan, COUNTRY=CN |NAME=LI Changdong, CITY=Foshan, COUNTRY=CN |NAME=ZHANG Xuemei, CITY=Foshan, COUNTRY=CN |NAME=ZHONG Yingsheng, CITY=Foshan, COUNTRY=CN|(WO2023/087800)|NAME=YU, Haijun No. 6 Zhixin Avenue, Leping Town, Sanshui District Foshan, Guangdong 528137, POSTCODE=528137, COUNTRY=CN |NAME=LI, Aixia No. 6 Zhixin Avenue, Leping Town, Sanshui District Foshan, Guangdong 528137, POSTCODE=528137, COUNTRY=CN |NAME=XIE, Yinghao No. 6 Zhixin Avenue, Leping Town, Sanshui District Foshan, Guangdong 528137, POSTCODE=528137, COUNTRY=CN |NAME=LI, Changdong No. 6 Zhixin Avenue, Leping Town, Sanshui District Foshan, Guangdong 528137, POSTCODE=528137, COUNTRY=CN |NAME=ZHANG, Xuemei No. 6 Zhixin Avenue, Leping Town, Sanshui District Foshan, Guangdong 528137, POSTCODE=528137, COUNTRY=CN |NAME=ZHONG, Yingsheng No. 6 Zhixin Avenue, Leping Town, Sanshui District Foshan, Guangdong 528137, POSTCODE=528137, COUNTRY=CN|(GB2620690)|NAME=Haijun Yu|NAME=Aixia Li|NAME=Yinghao Xie|NAME=Changdong Li|NAME=Xuemei Zhang|NAME=Yingsheng Zhong|(GB2620690)|NAME=Haijun Yu|NAME=Aixia Li|NAME=Yinghao Xie|NAME=Changdong Li|NAME=Xuemei Zhang|NAME=Yingsheng Zhong|(GB2620690)|NAME=Haijun Yu|NAME=Aixia Li|NAME=Yinghao Xie|NAME=Changdong Li|NAME=Xuemei Zhang|NAME=Yingsheng Zhong|(DE112022000199)|NAME=Yu Haijun, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Li Aixia, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Xie Yinghao, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Li Changdong, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Zhang Xuemei, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Zhong Yingsheng, CITY=Foshan, STATE=Guangdong , COUNTRY=CN|(DE112022000199)|NAME=Yu Haijun, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Li Aixia, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Xie Yinghao, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Li Changdong, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Zhang Xuemei, CITY=Foshan, STATE=Guangdong , COUNTRY=CN |NAME=Zhong Yingsheng, CITY=Foshan, STATE=Guangdong , COUNTRY=CN|(CN114229816)|NAME=YU HAIJUN|NAME=LI AIXIA|NAME=XIE YINGHAO|NAME=LI ZHANGDONG|NAME=ZHANG XUEMEI|NAME=ZHONG YINGSHENG|(CN114229816)|NAME=YU HAIJUN|NAME=LI AIXIA|NAME=XIE YINGHAO|NAME=LI ZHANGDONG|NAME=ZHANG XUEMEI|NAME=ZHONG YINGSHENG|(HU231541)|NAME=Yu Haijun|NAME=Li Aixia|NAME=Xie Yinghao|NAME=Li Changdong|NAME=Zhang Xuemei|NAME=Zhong Yingsheng|(HUP2300206)|NAME=Yu Haijun|NAME=Li Aixia|NAME=Xie Yinghao|NAME=Li Changdong|NAME=Zhang Xuemei|NAME=Zhong Yingsheng|(MX415021)|NAME=Haijun YU, COUNTRY=CN |NAME=Aixia LI, COUNTRY=CN |NAME=Yinghao XIE, COUNTRY=CN |NAME=Changdong LI, COUNTRY=CN |NAME=Xuemei ZHANG, COUNTRY=CN |NAME=Yingsheng ZHONG, COUNTRY=CN|(MX2023014158)|NAME=LI Changdong|NAME=YU Haijun|NAME=ZHONG Yingsheng|NAME=XIE Yinghao|NAME=ZHANG Xuemei|NAME=LI Aixia|(ES2963369)|NAME=YU, Haijun|NAME=LI, Aixia|NAME=XIE, Yinghao|NAME=LI, Changdong|NAME=ZHANG, Xuemei|NAME=ZHONG, Yingsheng|(ES2963369)|NAME=YU, Haijun|NAME=LI, Aixia|NAME=XIE, Yinghao|NAME=LI, Changdong|NAME=ZHANG, Xuemei|NAME=ZHONG, Yingsheng 9 8 Titre: (US12009492)|Method for recycling and preparing positive electrode material from waste lithium iron phosphate batteries Résumé: (US12009492)|A method for recycling and preparing a positive electrode material from waste lithium iron phosphate batteries. The method comprises the following steps: discharging, crushing, and stripping waste lithium iron phosphate batteries to obtain black powder; then mixing the black powder with benzenesulfonate, and reacting in a fluidized bed; and then adding an acid and an alkali to remove impurities, finally adding a lithium supplement, an iron supplement, or a phosphate, and a reducing agent, and sintering. According to the method, by controlling and optimizing the crushing, stripping, carbon and fluorine removal, and impurity removal processes, a positive electrode material with high purity can be recycled while controlling the recycling cost, and batteries prepared by means of the recycled positive electrode material have good performance. 106 Abstract gpt-4o-mini no The article focuses on recycling materials from lithium iron phosphate batteries and does not address accelerated weathering or CO₂ capture.
102 CN202211274086 WOCN2023/116687|CN202211274086 WO2024/082838|CN115628106|CN115628106 103532840 WO2024/082838 A1 2024-04-25 [WO202482838]|CN115628106 B 2023-05-19 [CN115628106B]|CN115628106 A 2023-01-20 [CN115628106] 2022-10-18 2023-09-04|2022-10-18 2024-04-25|2023-05-19|2023-01-20 |(CN115628106B)|2023-05-19 (WO2024/082838)|2026-04-18|(CN115628106)|2042-10-18 (WO2024/082838)|Method for synergistic fluidization filling disposal of solid mine waste and carbon dioxide storage (WO2024/082838)|Disclosed are a method for synergistic fluidization filling disposal of solid mine waste and carbon dioxide storage and a system based on the method. In the method, a ground carbon sequestration-ground well filling-downhole carbon sequestration system is formed, and a solid mine waste-based filling slurry (12) with a CO2 mineralization storage function is introduced into a goaf which is formed after coal resources are mined, thereby realizing the disposal of solid mine waste and CO2 storage. The method specifically comprises: mixing crushed coal gangue with an additive, conveying the mixture to a stirring carbon sequestration reaction device (7), adding water thereto and stirring same, injecting CO2 gas into same from the bottom, and stopping injecting CO2 after the flowing performance of the slurry reaches the minimum limit required by pumping; conveying the filling slurry to a downhole goaf (11) by means of a filling pump (9) via a filling pipeline (10); and after the downhole goaf is filled with the filling slurry, injecting CO2 into the downhole slurry via a gas pipeline (13) until the slurry is solidified. The method is safe, efficient and feasible, has low costs, achieves green mining of coal resources and CO2 storage in a downhole space, and reduces the damage of coal mining to the ecological environment. CHINA UNIVERSITY OF MINING & TECHNOLOGY (WO2024/082838)|CHINA UNIVERSITY OF MINING AND TECHNOLOGY ([CN])|(CN115628106)|CHINA UNIVERSITY OF MINING & TECHNOLOGY ([CN])|(CN115628106)|CHINA UNIVERSITY OF MINING & TECHNOLOGY ([CN]) LI BAIYI|LONG KANG|GUO YUMING|ZHANG JIXIONG|MA JIAYUAN|ZHOU NAN (WO2024/082838)|LI, Baiyi|LONG, Kang|GUO, Yuming|ZHANG, Jixiong|MA, Jiayuan|ZHOU, Nan (WO2024/082838)|NANJING JINGWEI PATENT & TRADEMARK AGENCY CO., LTD ([CN])|(CN115628106)|GUO LINA;NANJING JINGWEI PATENT & TRADEMARK AGENCY CO., LTD|Reg. Nb: 32200 (WO2024/082838)|The invention has the advantages that:|Therefore, the prior art has the advantages that the amount of the coal gangue consumed in the well sealing is small, the waste such as the coal gangue can not be reasonably treated after the well sealing is carried out, the auxiliary filling material of the large-scale equipment in the well is fully mineralized after the well sealing is discarded in the well sealing, and the well sealing is limited by the sealing space, so that the small sealing amount can only be realized.|At present, the key technology of using coal gangue, tailings and other materials for mineralization and carbon dioxide adsorption is mainly concentrated in the addition of effective additives, but this kind of method can only consume a small amount of coal gangue or end the CO2 sequestration process of waste coal gangue difficult to be reasonably disposed. For example, "a system for removing flue gas CO2 from a power plant by using a modified coal gangue and an implementation method thereof" uses an organic amine active component to spray and load on the modified broken coal gangue to capture CO2, the CO2 capture effect is good, but the CO22 finally used as a carrier is still difficult to be reasonably disposed. But the technology which is related to underground treatment of coal gangue and synchronous sequestration often transport the filling material to the underground and then carry out the carbon injection and other processes and lose the advantages of mineralization in the well, or is limited by the storage space and can only achieve a small storage. For example, the system and method for "short-long-wall intermittent filling and mining synergistic alkali-based solid CO2 storage" fill the prepared filling material into the short-wall working surface of the well and then carry out carbon filling and storage, and discard the advantage conditions of full mineralization of auxiliary filling material of large-scale equipment on the well; for example, "a method for waste treatment and carbon dioxide storage of coal-fired power plants at the pit" adopts gangue, cement and alkaline aqueous solution to directly capture the CO2 of the power plant and then fill the waste wellbore, the filling space and the storage amount of which are limited by the capacity of the waste wellbore.|In the face of the pressure of ecological environment protection, how to deal with solid waste such as coal gangue efficiently is one of the problems faced by the high quality development of coal enterprises. On the other hand, climate change is a global problem facing mankind, CO2 emissions are increasing, and it is a threat to life systems.| (WO2024/082838)|1. The invention relates to a collaborative carbon dioxide sealing method for solid waste fluidization, filling and disposal of mines, which is characterized in that a ground carbon fixing-ground well filling-underground carbon fixing system is formed in sequence based on the mineralization characteristics of gangue solid waste and CO2, a mine solid waste base filling slurry with the function of mineralization and sealing CO2 is filled into a mined area formed after the mining of coal resources, and the mine solid waste disposal and the CO2 sealing are realized, the concrete steps are as follows: a, the preparation of filling materials: the gangue is crushed in a crushing workshop and a grinding workshop, and then the gangue is crushed The feeding machine mixes the crushed and ground coal gangue with the additive in each additive material bin and delivers the mixture to the stirring carbon fixation reaction device; b, the ground carbon fixation: the feeding machine adds a certain amount of water into the stirring carbon fixation reaction device to start stirring, and starts to inject CO2 gas from the bottom of the stirring carbon fixation reaction device through a CO2 gas source, and after the flow performance of the filling slurry reaches the minimum requirement of pumping, the carbon fixation reaction device Stop stirring and stop injecting CO2; c, fluidizing filling: power is provided by the filling pump, and the stirred filling slurry is transported to the underground mining space through the filling pipeline of the ground-well drilling hole; d, the underground carbon fixation: after the filling slurry is filled with the underground mining space, the CO2 ground-well injection system is opened, and the CO2 is injected into the inner part of the underground filling slurry through the gas pipeline, until the filling slurry is consolidated, and the fluidizing solid waste filling treatment and the CO2 sealing of the underground mining space in the mining area are realized.|2. The invention is characterized in that in step b, the coal gangue crushing needs to meet the pumping requirement of filling slurry, the particle diameter of the coal gangue is less than 10mm, and the proportion of the coal gangue below 2mm is not less than 1/3.|3. The invention is characterized in that in step b, the stirring reaction time of CO2 and filling slurry in the stirring carbon fixation reaction device is determined according to the flow performance of the filling slurry and monitored by an automatic viscosity measuring instrument.|4. The invention is characterized in that in step b, the coal gangue is 60-80wt%, the additive accounts for 5wt% of the coal gangue, and the rest is water.|5. The method is characterized in that in step d, the phase state of the filling slurry can be judged by the CO2 injection pressure and flow rate; when the CO2 injection pressure increases rapidly and the flow rate is unchanged, the filling slurry is judged to be consolidated and the CO2 injection can be stopped.|6. The invention is characterized in that the additive comprises fly ash, lime and magnesium slag powder, preferably magnesium slag powder and lime powder, and is used for increasing carbon sequestration effect.| (WO2024/082838)|The invention aims at a collaborative carbon dioxide sealing method for the fluidization, filling and disposal of solid wastes in a mine, which is based on the mineralization characteristics of gangue solid wastes and CO2, sequentially forms a ground carbon fixing, ground well filling and underground carbon fixing system, and fills a mined area formed after the mining of coal resources with a mine solid waste base filling slurry with the function of mineralization and sealing CO2, thus realizing the solid wastes disposal and the sealing of CO2 in a mine, and specifically comprises the following steps:|The invention aims at providing a synergistic carbon dioxide sealing method for the fluidization, filling and disposal of solid waste in mines, which sequentially forms a ground carbon fixing-ground well filling-underground carbon fixing system based on the mineralization characteristics of the solid waste of coal gangue and CO2, prepares a filling slurry with coal gangue and additives, fully mixes and stirs the slurry with CO2, and then fills the underground extraction space and fills the CO2, This method is safe, efficient, practical, and low-cost.|The invention relates to the field of coal mine green mining and carbon storage, in particular to a synergistic carbon dioxide storage method for solid waste fluidization, filling and treatment in a mine.| (WO2024/082838)|COAL GANGUE(100,32)|SOLID WASTE(100,20)|CARBON DIOXIDE(100,13)|FILLING(100,13)|CARBON DIOXIDE SEALING(100,8)|CARBON DIOXIDE STORAGE(100,4)|MINE DISPOSAL(100,3)|SOLID WASTE FLUIDIZATION(100,3)|FILLING DISPOSAL(100,1)|FLUIDIZATION FILLING DISPOSAL(100,1)|SOLID(100,1)|SYNERGISTIC FLUIDIZATION FILLING DISPOSAL(100,1)|FILLING SLURRY(63,37)|COAL RESOURCE MINING(59,4)|COAL GANGUE CRUSHING(50,2)|COAL GANGUE UNDERGROUND TREATMENT(46,1)|COAL RESOURCE(44,8)|PIPELINE FILLING(43,16)|COAL GANGUE PROPORTION(43,2)|GRINDING WORKSHOP(40,12)|DOWNHOLE GOAF(40,2)|WASTE COAL GANGUE(40,1)|WASTE WELLBORE(38,2)|CRUSHED COAL GANGUE(38,1)|COAL MINE GREEN MINING(36,1)|SYNCHRONOUS SEQUESTRATION(36,1)|CRUSHING WORKSHOP(33,8)|COAL ENTERPRISE QUALITY DEVELOPMENT(33,1)|FLUIDIZING FILLING(33,1)|UNDERGROUND FILLING SLURRY(32,3)|AUXILIARY FILLING(31,2)|COAL ENTERPRISE(31,1)|COAL RESOURCE GREEN MINING(30,3)|SEALING CO2(30,2)|AUXILIARY FILLING FULL MINERALIZATION(30,1)|MODIFIED COAL GANGUE(30,1)|CO2 SEALING(29,3)|GANGUE(28,4)|FILLING SLURRY PUMPING REQUIREMENT(28,3)|COAL GANGUE PARTICLE DIAMETER(28,2)|CO2(27,36)|FILLING PUMP(27,12)|STIRRED FILLING SLURRY(27,2)|UNDERGROUND MINING SPACE(26,11)|MINERALIZATION FUNCTION(26,2)|LIME POWDER(26,1)|MODIFIED BROKEN COAL GANGUE(26,1)|PUMPING MINIMUM REQUIREMENT(26,1)|CO2 INJECTION(25,6)|GREEN MINING(25,4)|MINERALIZATION(25,2)|CARBON FIXATION REACTION(24,16)|MINE(24,7)|DOWNHOLE SLURRY(24,1)|WASTE FILLING SLURRY(24,1)|ADDITIVE ACCOUNT(22,2)|CO2 EMISSION(22,1)|COAL GANGUE SOLID WASTE(22,1)|FULL MINERALIZATION(22,1)|UNDERGROUND EXTRACTION SPACE(22,1)|UNDERGROUND TREATMENT(22,1)|CARBON FIXATION(21,32)|GROUND GANGUE MOUNTAIN(20,3)|PUMPING REQUIREMENT(20,3)|UNDERGROUND CARBON FIXATION(20,2)|FLUIDIZATION(19,8)|DISPOSAL(19,7)|BASE FILLING SLURRY(19,4)|CONCRETE(19,1)|FLUIDIZING SOLID WASTE(19,1)|MINIMUM REQUIREMENT(19,1)|UNDERGROUND CARBON FIXING(19,1)|MINED AREA(18,2)|COAL MINING DAMAGE(18,1)|ECOLOGICAL ENVIRONMENT PROTECTION(18,1)|GANGUE SOLID WASTE(18,1)|ADDITIVE(17,7)|MINE SOLID WASTE(17,5)|QUALITY DEVELOPMENT(17,1)|SLURRY FLOWING PERFORMANCE(17,1)|UNDERGROUND(17,1)|CARBON SEQUESTRATION(16,11)|AUTOMATIC VISCOSITY MEASURING INSTRUMENT(16,2)|SLURRY(16,2)|CARBON DIOXIDE ADSORPTION(16,1)|CARBON INJECTION(16,1)|FILLING PREPARATION(16,1)|STIRRING CARBON SEQUESTRATION(16,1)|FILLING SLURRY FLOW PERFORMANCE(15,5)|VISCOSITY MEASURING INSTRUMENT(15,2)|ALKALINE AQUEOUS SOLUTION(15,1)|CARBON FILLING(15,1)|CARBON FIXING(14,7)|MAN(14,1)|TAILING(14,1)|THREAT(14,1)|WELL SEALING(13,5)|CO2 INJECTION PRESSURE(13,2)|MINE SOLID WASTE DISPOSAL(13,2)|PARTICLE DIAMETER(13,2)|COAL MINE(13,1)|DOWNHOLE SPACE(13,1)|FILLING SPACE(13,1)|GAS PIPELINE(12,16)|UNDERGROUND MINING(12,10)|CO2 SEQUESTRATION(12,6)|CEMENT(12,1)|CO2 MINERALIZATION STORAGE FUNCTION(12,1)|ECOLOGICAL ENVIRONMENT PROTECTION PRESSURE(12,1)|SOLID CO2 STORAGE(12,1)|ADDITIVE MATERIAL BIN(11,7)|CARBON STORAGE(11,1)|GROUND CARBON FIXING(11,1)|INJECTING CO2 GAS(11,1)|POWER PLANT CO2(11,1)|REMOVING FLUE GAS(11,1)|SEALING(11,1)|FEEDER(10,5)|GROUND CARBON FIXATION(10,5)|LIME(10,2)|PERFORMING FLOW(9,6)|FLY ASH(9,3)|MINING(9,3)|CO2 CAPTURE EFFECT(9,1)|SMALL SEALING(9,1)|POWER PLANT(8,2)|AMINE ACTIVE COMPONENT(8,1)|MINIMUM LIMIT(8,1)|ORGANIC AMINE ACTIVE COMPONENT(8,1)|REACTION DEVICE STOP STIRRING(8,1)|WASTE TREATMENT(8,1)|STIRRING CARBON FIXING REACTION(7,4)|WATER BIN(7,3)|CLIMATE CHANGE(7,1)|CO2 GAS SOURCE(6,9)|LARGE SCALE EQUIPMENT(6,2)|GANGUE MOUNTAIN SPONTANEOUS COMBUSTION(6,1)|MINERALIZATION SEQUESTRATION(6,1)|SHORT WALL WORKING(6,1)|MINING AREA(5,10)|FILLING MATERIAL(5,5)|CO2 STIRRING REACTION TIME(5,1)|COAL FIRED POWER PLANT(5,1)|CONSTRUCTING ECOLOGICAL CIVILIZATION(5,1)|DEEP GEOLOGICAL RESERVOIR(5,1)|SCARCE LAND RESOURCE(5,1)|SMALL STORAGE(5,1)|CO2 GAS(4,5)|SOLID WASTE DISPOSAL(4,5)|CARBONATE MINERAL(4,2)|DOWNHOLE CARBON SEQUESTRATION(4,2)|GEOLOGICAL SEALING(4,2)|UNDERGROUND CARBON SEQUESTRATION(4,2)|ACTIVE COMPONENT(4,1)|AGITATED FILLING SLURRY(4,1)|STORAGE SPACE(4,1)|SYNERGISTIC CO2 SEQUESTRATION(4,1)|UNDERGROUND FILLING SLURRY INTERIOR(4,1)|CO2 GEOLOGICAL STORAGE(3,1)|COAL MINE ENGINEERING(3,1)|DEVELOPING CO2 CAPTURE(3,1)|POROUS ADSORPTION(3,1)|SOLIDIFY CO2(3,1)|STIRRED REACTION TIME(3,1)||(CN115628106)|SOLID WASTE(100,30)|COAL GANGUE(100,28)|FLUIDIZATION(100,13)|CARBON DIOXIDE(100,11)|MINE SOLID WASTE(100,10)|CARBON DIOXIDE SEALING(100,6)|DISPOSAL(100,2)|SOLID WASTE FLUIDIZATION(100,1)|CRUSHING COAL GANGUE(84,1)|COAL RESOURCE GREEN EXPLOITATION(83,3)|PIPELINE FILLING(77,17)|ABOVEGROUND SEALING(71,3)|CRUSHING WORKSHOP(70,10)|UNDERGROUND EXTRACTION SPACE(68,8)|COAL EXPLOITATION DAMAGE(67,2)|COAL GANGUE UNDERGROUND TREATMENT(65,1)|FILLING SLURRY(64,23)|MIXING CRUSHED GANGUE(64,1)|GRINDING WORKSHOP(63,12)|GREEN EXPLOITATION(58,4)|COAL RESOURCE EXPLOITATION(57,5)|COAL MINE GREEN EXPLOITATION(57,1)|WASTE COAL GANGUE(57,1)|UNDERGROUND SLURRY(56,1)|MINERALIZATION SEALING(51,4)|COAL EXPLOITATION(51,3)|FLUIDIZATION FILLING(48,1)|SLURRY(47,6)|COAL RESOURCE(44,3)|COAL ENTERPRISE(44,1)|RATIONAL DISPOSAL(44,1)|UNDERGROUND FILLING SLURRY(43,3)|FUNCTIONAL MINE(42,5)|STIRRING CARBON FIXING REACTION(41,20)|MODIFIED COAL GANGUE(41,1)|GANGUE(40,6)|MINERALIZATION FEATURE(40,1)|GROUND GANGUE HILL(39,3)|CARBON FIXATION(37,34)|FILLING PUMP(37,11)|UNDERGROUND SEALING(37,1)|ECOLOGICAL ENVIRONMENT(36,4)|DISCONTINUOUS FILLING(36,1)|DOWNHOLE CARBON FIXATION(36,1)|GANGUE RATIO(36,1)|MODIFIED BROKEN COAL GANGUE(36,1)|PIT MOUTH(36,1)|ADDITIVE(35,11)|STIRRED FILLING SLURRY(35,3)|FILLING SLURRY PHASE(35,1)|GROUND CARBON FIXATION(34,10)|UNDERGROUND EXTRACTION(34,5)|FEEDER(33,11)|CARBON STRENGTHENING(33,2)|CARBON FIXING REACTION(32,21)|SYNCHRONOUS SEALING(32,1)|MINE MINING AREA(31,2)|UNDERGROUND TREATMENT(31,1)|TECHNICAL DEFECT(30,1)|MINERALIZATION(29,5)|STOPPING STIRRING(29,2)|UNDERGROUND SPACE(29,2)|STIRRING START(29,1)|BASE FILLING SLURRY(28,5)|FUNCTIONAL MINE SOLID WASTE(28,5)|WASTE TREATMENT(28,1)|FILLER SLURRY(27,8)|GOAF(25,5)|ECOLOGICAL ENVIRONMENT PROTECTION(25,1)|CAPTURE(24,1)|CARBON INJECTION SEALING(24,1)|DOWNHOLE PRODUCTION(23,4)|TECHNICAL KEY(23,1)|PUMPING(22,4)|COAL GANGUE SOLID WASTE(22,3)|ALKALINE AQUEOUS SOLUTION(22,1)|UNDERGROUND(22,1)|CARBON INJECTION(21,1)|STOPPING(21,1)|GAS PIPELINE(20,14)|AUTOMATIC VISCOSITY MEASURING INSTRUMENT(20,3)|UNDERGROUND MINING(20,3)|TAILING(20,1)|THREAT(20,1)|ADDITIVE MATERIAL BIN(19,7)|VISCOSITY MEASURING INSTRUMENT(19,3)|FLUIDIZED SOLID WASTE(19,2)|INJECTION PRESSURE(18,6)|DOWNHOLE PRODUCTION SPACE(18,3)|SMALL SEALING(18,2)|COAL MINE(18,1)|FILLING SPACE(18,1)|FILLING MATERIAL(17,4)|QUICKLIME(17,4)|CEMENT(17,1)|ECOLOGICAL ENVIRONMENT PROTECTION PRESSURE(17,1)|WATER BIN(16,4)|CARBON FIXATION REACTION(15,6)|SOLID WASTE DISPOSAL(15,5)|WASTE WELL BORE(14,2)|FLY ASH(13,3)|CRUSHED COAL GANGUE(13,2)|SYNERGISTIC BASE SOLID WASTE(13,1)|CARBON SEQUESTRATION(11,3)|POWER PLANT(11,2)|ABOVEGROUND LARGE SCALE EQUIPMENT(11,1)|AMINE ACTIVE COMPONENT(11,1)|CLIMATE CHANGE(11,1)|COAL GANGUE CRUSHING(11,1)|FLUE GAS(11,1)|LONG WALL DISCONTINUOUS FILLING(11,1)|ORGANIC AMINE ACTIVE COMPONENT(11,1)|GEOLOGICAL SEQUESTRATION(10,2)|PREPARED FILLING MATERIAL(10,1)|WASTE WELL BORE CAPACITY(10,1)|WIDE APPLICATION PROSPECT(10,1)|COAL GANGUE RATIO(9,3)|FILLING SLURRY PUMPING REQUIREMENT(9,2)|GANGUE MOUNTAIN SPONTANEOUS COMBUSTION(9,1)|SCARCE LAND RESOURCE(9,1)|TREATMENT COCARBON DIOXIDE SEQUESTRATION(8,1)|GAS SOURCE(7,6)|AIR SOURCE(7,3)|POROUS ADSORPTION(7,2)|COAL FIRED POWER PLANT(7,1)|CONSTRUCTING ECOLOGICAL CIVILIZATION(7,1)|DEEP GEOLOGICAL RESERVOIR(7,1)|DOWNHOLE FILLER SLURRY(7,1)|INFRASTRUCTURE FILLING FACILITY(7,1)|TOTHE FILLER SLURRY(7,1)|GEOLOGICAL SEALING(6,2)|ACTIVE COMPONENT(6,1)|COCARBON DIOXIDE SEALING(6,1)|EMISSION STRATEGIC SELECTION(6,1)|LARGE SCALE EQUIPMENT(6,1)|SOLIDIFIED FILLING SLURRY(6,1)|UNDERGROUND EXTRACTION MIDDLE(6,1)|WALL WORKING SURFACE(6,1)|PARTICLE SIZE(5,4)|COAL MINE ENGINEERING(5,1)|DOWNHOLE EXTRACTION(5,1)|GANGUE HILL(5,1)|GROUND ACCUMULATED GANGUE(5,1)|MAGNESIUM SLAG POWDER(5,1)|REACTED FILLING SLURRY(5,1)|FLOW RATE(4,6)|CARBONATE MINERAL(4,1)|COAL ENERGY STATUS(4,1)|COAL YIELD(4,1)|HIGH QUALITY DEVELOPMENT(4,1)|QUICKLIME POWDER(4,1)|RICH COAL(4,1)|UNDERGROUND CARBON SEQUESTRATION(4,1)|CHARGE SLURRY BOTTOM(3,2)|COAL GANGUE PARTICLE SIZE(3,2)|MINING AREA ECOLOGICAL ENVIRONMENT(3,2)|PIPELINE(3,2)|STIRRING REACTION TIME(3,2)|CHARGE SLURRY PHASE(3,1)|COAL EXTRACTION DAMAGE(3,1)|COAL MINE EXTRACTION SPACE(3,1)|FOUNDATION PREPARATION(3,1)||(CN115628106)|COAL GANGUE(100,34)|SOLID WASTE(100,34)|CARBON DIOXIDE(100,19)|CARBON DIOXIDE SEQUESTRATION(100,13)|MINE SOLID WASTE(100,13)|DISPOSAL(100,6)|FLUIDIZATION(100,6)|CRUSHED COAL GANGUE(60,1)|COAL RESOURCE GREEN MINING(55,3)|CRUSHING COAL GANGUE(47,2)|FILLING SLURRY(43,26)|WASTE COAL GANGUE(43,1)|MINERALIZATION SEQUESTRATION(40,3)|UNDERGROUND SLURRY(40,1)|FLUIDIZED FILLING TREATMENT(39,6)|MODIFIED CRUSHED COAL GANGUE(37,1)|GRINDING WORKSHOP(36,11)|GREEN MINING(36,4)|PIPELINE FILLING(35,16)|UNDERGROUND EXTRACTION SPACE(35,9)|MINE FLUIDIZED FILLING DISPOSAL(35,1)|CRUSHING WORKSHOP(33,9)|SLURRY(32,7)|UNDERGROUND FILLING SLURRY(32,3)|COAL ENTERPRISE(31,1)|MODIFIED COAL GANGUE(31,1)|COAL GANGUE CRUSHING(30,3)|CARBON FIXATION REACTION(29,22)|COAL RESOURCE(29,4)|UNDERGROUND PRODUCTION(28,5)|COAL RESOURCE EXPLOITATION(28,3)|FLUIDIZATION FILLING TREATMENT(28,1)|COAL GANGUE SOLID WASTE(27,4)|ECOLOGICAL ENVIRONMENT(26,4)|ADDITIVE(25,12)|COAL MINING DAMAGE(25,3)|STIRRED FILLING SLURRY(25,3)|INTERMITTENT FILLING(25,1)|MINE SOLID WASTE SEQUESTRATION(25,1)|ABANDONED SHAFT(23,2)|AUXILIARY FILLING(23,1)|COAL MINE CARBON SEQUESTRATION(23,1)|CARBON FIXATION(22,36)|CARBON SEQUESTRATION(22,23)|FLUIDIZED FILLING(22,3)|FILLING PUMP(21,10)|BASE FILLING SLURRY(21,4)|FILLING TREATMENT(21,2)|STOPPING STIRRING(21,2)|UNDERGROUND SPACE(21,2)|STIRRING START(21,1)|TECHNICAL DEFECT(21,1)|FEEDER(20,9)|GROUND CARBON SEQUESTRATION(20,4)|UNDERGROUND PRODUCTION TREATMENT(20,2)|UNDERGROUND PRODUCTION SPACE(20,1)|WASTE TREATMENT(20,1)|UNDERGROUND CARBON SEQUESTRATION(19,6)|FILLING SLURRY PUMPING REQUIREMENT(19,3)|GROUND GANGUE DUMP(19,3)|MINERALIZATION COMBINED ACTION(19,1)|SAMESPRAYING(19,1)|ABANDONED SHAFT CAPACITY(18,1)|ECOLOGICAL ENVIRONMENT PROTECTION(18,1)|CARBON INJECTION SEALING(17,1)|TECHNICAL KEY(17,1)|PUMPING(16,4)|COAL GANGUE RATIO(16,3)|MINERALIZATION(16,3)|FILLING PREPARATION(16,1)|QUICKLIME POWDER(15,2)|ALKALINE AQUEOUS SOLUTION(15,1)|UNDERGROUND MINING(14,3)|FLUIDIZATION SOLID WASTE(14,2)|TAILING(14,1)|THREAT(14,1)|COAL MINING(13,5)|FILLING SPACE(13,1)|GAS PIPELINE(12,14)|SEALED STORAGE(12,3)|CEMENT(12,1)|DIRECTLY CAPTURED OIL(12,1)|ECOLOGICAL ENVIRONMENT PROTECTION PRESSURE(12,1)|ADDITIVE MATERIAL BIN(11,8)|FILLING SLURRY FLOW PROPERTY(11,5)|GOAF(11,4)|COAL MINE(11,2)|CARBON DIOXIDE(11,1)|FINISHING(11,1)|WALL WORKING FACE(11,1)|AUTOMATIC VISCOSITY MEASURING INSTRUMENT(10,2)|COORDINATION(10,1)|COAL GANGUE PARTICLE SIZE(9,3)|BALANCE WATER(9,1)|GREEN MINING FIELD(9,1)|INJECTION PRESSURE(8,7)|SOLID WASTE DISPOSAL(8,5)|ACTION COMBINATION(8,2)|POWER PLANT(8,2)|AMINE ACTIVE COMPONENT(8,1)|BASIC SOLID WASTE(8,1)|COAL GANGUE MINE ACCUMULATION(8,1)|LONG WALL INTERMITTENT FILLING(8,1)|ORGANIC AMINE ACTIVE COMPONENT(8,1)|GAS SOURCE(7,8)|WATER BIN(7,4)|FILLING MATERIAL(7,2)|CLIMATE CHANGE(7,1)|FLUE GAS(7,1)|GROUND SURFACE(7,1)|WIDE APPLICATION PROSPECT(7,1)|FLY ASH(6,3)|UNDERGROUND EXTRACTION(6,3)|LARGE SCALE EQUIPMENT(6,2)|SMALL SEALING(6,2)|SCARCE LAND RESOURCE(6,1)|MINING AREA(5,10)|GEOLOGICAL SEALING(5,3)|COAL FIRED POWER PLANT(5,1)|COAL GANGUE PROPORTION(5,1)|CONSTRUCTING ECOLOGICAL CIVILIZATION(5,1)|DEEP GEOLOGICAL RESERVOIR(5,1)|DOWNHOLE FILLER SLURRY(5,1)|GANGUE HILL SPONTANEOUS COMBUSTION(5,1)|GEOLOGICAL SEQUESTRATION(5,1)|STIRRING SOLID CARBON REACTION(5,1)|UNDERGROUND COAL GANGUE TREATMENT(5,1)|CARBONATE MINERAL(4,2)|GROUND WELL DRILLING(4,2)|ACTIVE COMPONENT(4,1)|EMISSION STRATEGIC SELECTION(4,1)|SOLIDIFIED FILLING SLURRY(4,1)|REACTING CARBON SEQUESTRATION(3,4)|UNDERGROUND CARBON FIXATION(3,2)|CAPTURE UTILIZATION(3,1)|COAL MINE ENGINEERING(3,1)|CREATIVE EFFORT(3,1)|HIGH QUALITY DEVELOPMENT(3,1)|MAGNESIUM SLAG POWDER(3,1)|OCEAN SEALING(3,1)|UNDERGROUND PRODUCTION DISPOSAL(3,1)|MINE MINING AREA(2,3)|DOWNHOLE PRODUCTION SPACE(2,2)|FUNCTIONAL MINE SOLID WASTE(2,2)|MINING AREA ECOLOGICAL ENVIRONMENT(2,2)|BASIC FILLING FACILITY(2,1)|COAL YIELD(2,1)| (WO2024/082838)|1. The invention relates to a collaborative carbon dioxide sealing method for solid waste fluidization, filling and disposal of mines, which is characterized in that a ground carbon fixing-ground well filling-underground carbon fixing system is formed in sequence based on the mineralization characteristics of gangue solid waste and CO2, a mine solid waste base filling slurry with the function of mineralization and sealing CO2 is filled into a mined area formed after the mining of coal resources, and the mine solid waste disposal and the CO2 sealing are realized, the concrete steps are as follows: |a, the preparation of filling materials: the gangue is crushed in a crushing workshop and a grinding workshop, and then the gangue is crushed The feeding machine mixes the crushed and ground coal gangue with the additive in each additive material bin and delivers the mixture to the stirring carbon fixation reaction device; |b, the ground carbon fixation: the feeding machine adds a certain amount of water into the stirring carbon fixation reaction device to start stirring, and starts to inject CO2 gas from the bottom of the stirring carbon fixation reaction device through a CO2 gas source, and after the flow performance of the filling slurry reaches the minimum requirement of pumping, the carbon fixation reaction device Stop stirring and stop injecting CO2; |c, fluidizing filling: power is provided by the filling pump, and the stirred filling slurry is transported to the underground mining space through the filling pipeline of the ground-well drilling hole; |d, the underground carbon fixation: after the filling slurry is filled with the underground mining space, the CO2 ground-well injection system is opened, and the CO2 is injected into the inner part of the underground filling slurry through the gas pipeline, until the filling slurry is consolidated, and the fluidizing solid waste filling treatment and the CO2 sealing of the underground mining space in the mining area are realized.|2. The invention is characterized in that in step b, the coal gangue crushing needs to meet the pumping requirement of filling slurry, the particle diameter of the coal gangue is less than 10mm, and the proportion of the coal gangue below 2mm is not less than 1/3.|3. The invention is characterized in that in step b, the stirring reaction time of CO2 and filling slurry in the stirring carbon fixation reaction device is determined according to the flow performance of the filling slurry and monitored by an automatic viscosity measuring instrument.|4. The invention is characterized in that in step b, the coal gangue is 60-80wt%, the additive accounts for 5wt% of the coal gangue, and the rest is water.|5. The method is characterized in that in step d, the phase state of the filling slurry can be judged by the CO2 injection pressure and flow rate; when the CO2 injection pressure increases rapidly and the flow rate is unchanged, the filling slurry is judged to be consolidated and the CO2 injection can be stopped.|6. The invention is characterized in that the additive comprises fly ash, lime and magnesium slag powder, preferably magnesium slag powder and lime powder, and is used for increasing carbon sequestration effect.|7. The invention relates to a system of a coordinated carbon dioxide sealing method for the fluidization, filling and disposal of solid waste in a mine based on the claim 1, in particular to a ground carbon fixing-ground well filling-underground carbon fixing system, which is arranged near a ground gangue mountain corresponding to the middle part of a mining area and comprises a feeder, a stirring carbon fixing reaction device, a filling pump and a filling pipeline which are connected in sequence, wherein, the feeder is respectively connected with a grinding workshop, a water bin and various additive material bins, the crushing workshop is connected with the grinding workshop, and the |filling pipeline is deep into the underground mining space, and the filling pipeline is connected with the grinding workshop The filling pipeline is provided with a filling pump; the filling pipeline and the gas pipeline are arranged in the well after the filling pump is drilled to the underground mining space; the CO2 gas source is connected with the gas pipeline, and the gas pipeline is divided into two sections of pipeline, one section is led into a stirring carbon fixation reaction device, and the other end is deep into the underground mining space. (WO2024/082838)|technical field|[0001] The invention relates to the field of coal mine green mining and carbon storage, in particular to a synergistic carbon dioxide storage method for solid waste fluidization, filling and treatment in a mine.|background technology|[0002] China's coal-rich, lean-oil and gas-poor energy characteristics determine the status of China's main energy. As the associated solid waste in coal mining, coal gangue usually discharges and deposits on the ground, accounting for 20% of the coal output. It not only occupies a large number of scarce land resources, causing a huge impact on the ecological environment of the mining area, but also will bring a series of potential safety hazards such as gangue mountain spontaneous combustion. In the face of the pressure of ecological environment protection, how to deal with solid waste such as coal gangue efficiently is one of the problems faced by the high quality development of coal enterprises.|[0003] On the other hand, climate change is a global problem facing mankind, CO2 emissions are increasing, and it is a threat to life systems. Developing CO2 capture, utilization and storage (CCUS) technology is not only a strategic choice for reducing CO2 emissions and ensuring energy security in the future, but also an important means for constructing ecological civilization and achieving sustainable development. CO2 sequestration is the process of CO2 capture into deep geological reservoir by engineering technology and realize long-term isolation of CO2 from the atmosphere.|[0004] At present, the key technology of using coal gangue, tailings and other materials for mineralization and carbon dioxide adsorption is mainly concentrated in the addition of effective additives, but this kind of method can only consume a small amount of coal gangue or end the CO2 sequestration process of waste coal gangue difficult to be reasonably disposed. For example, "a system for removing flue gas CO2 from a power plant by using a modified coal gangue and an implementation method thereof" uses an organic amine active component to spray and load on the modified broken coal gangue to capture CO2, the CO2 capture effect is good, but the CO22 finally used as a carrier is still difficult to be reasonably disposed.|[0005] But the technology which is related to underground treatment of coal gangue and synchronous sequestration often transport the filling material to the underground and then carry out the carbon injection and other processes and lose the advantages of mineralization in the well, or is limited by the storage space and can only achieve a small storage. For example, the system and method for "short-long-wall intermittent filling and mining synergistic alkali-based solid CO2 storage" fill the prepared filling material into the short-wall working surface of the well and then carry out carbon filling and storage, and discard the advantage conditions of full mineralization of auxiliary filling material of large-scale equipment on the well; for example, "a method for waste treatment and carbon dioxide storage of coal-fired power plants at the pit" adopts gangue, cement and alkaline aqueous solution to directly capture the CO2 of the power plant and then fill the waste wellbore, the filling space and the storage amount of which are limited by the capacity of the waste wellbore.|[0006] Therefore, the prior art has the advantages that the amount of the coal gangue consumed in the well sealing is small, the waste such as the coal gangue can not be reasonably treated after the well sealing is carried out, the auxiliary filling material of the large-scale equipment in the well is fully mineralized after the well sealing is discarded in the well sealing, and the well sealing is limited by the sealing space, so that the small sealing amount can only be realized.|[0007] Contents of Invention|[0008] The invention aims at providing a synergistic carbon dioxide sealing method for the fluidization, filling and disposal of solid waste in mines, which sequentially forms a ground carbon fixing-ground well filling-underground carbon fixing system based on the mineralization characteristics of the solid waste of coal gangue and CO2, prepares a filling slurry with coal gangue and additives, fully mixes and stirs the slurry with CO2, and then fills the underground extraction space and fills the CO2, This method is safe, efficient, practical, and low-cost. It can realize green mining of coal resources and underground space CO2 storage, reducing the damage to the ecological environment caused by coal mining, and has a broad application prospect.|[0009] At present, the use of CO2 mineralization principle is one of the main ways to achieve CO2 geological storage, that is, CO2 and rock occurred a rapid chemical reaction and formed a new carbonate minerals, through this method, CO2 was permanently "confined" in the rock, achieved CO2 mineralized geological storage.|[0010] The inventor discovers that the calcium magnesium compounds contained in solid wastes such as coal gangue can react with CO2 to form carbonate minerals, and therefore proposes a collaborative carbon dioxide sealing method for the fluidization, filling and disposal of solid wastes in mines, and the coal gangue solid wastes and the CO2 are simultaneously disposed and sealed in the coal mining space, which is of great significance for reducing the damage to the environment caused by coal mining and reducing the greenhouse gas emission, and conforms to the strategic goal of "double carbon" in China.|[0011] In order to realize the above-mentioned purpose, the invention adopts the following technical proposal:|[0012] The invention aims at a collaborative carbon dioxide sealing method for the fluidization, filling and disposal of solid wastes in a mine, which is based on the mineralization characteristics of gangue solid wastes and CO2, sequentially forms a ground carbon fixing, ground well filling and underground carbon fixing system, and fills a mined area formed after the mining of coal resources with a mine solid waste base filling slurry with the function of mineralization and sealing CO2, thus realizing the solid wastes disposal and the sealing of CO2 in a mine, and specifically comprises the following steps:|[0013] a. Preparation of filling materials: firstly, the coal gangue is crushed in a crushing workshop and a grinding workshop, and then the crushed and ground coal gangue is mixed with the additives in each additive material bin and transported to a stirring carbon fixation reaction device;|[0014] b. The process of carbon fixation on the ground: adding a certain amount of water to the stirring carbon fixation reaction device, starting stirring, and starting to inject CO2 gas from the bottom of the stirring carbon fixation reaction device through a CO2 gas source, and stopping stirring and stopping injecting CO2 after the flow performance of the filling slurry reaches the minimum required by pumping;|[0015] (c) Fluidization filling process: a filling pump is used to provide power, and the agitated filling slurry is transported to the underground mining space through a filling pipeline of a ground-well drilling hole;|[0016] d. Underground carbon sequestration working procedure: after the filling slurry fills the underground mining space, the CO2 ground-well injection system is opened, and the CO2 is injected into the inner part of the underground filling slurry through a gas pipeline until the filling slurry is consolidated, thereby realizing the fluidization solid waste filling treatment and the CO2 sealing of the underground mining space in the mining area.|[0017] Preferably, in step b, the coal gangue crushing needs to meet the pumping requirement of the filling slurry, the coal gangue particle size is less than 10mm, and the proportion of the coal gangue particle size less than 2 mm is not less than 1/3.|[0018] Preferably, in step b, the agitation reaction time of CO2 with the filler slurry in the agitation carbon fixation reaction apparatus is determined according to the flow performance of the filler slurry and monitored by a viscosity automatic meter.|[0019] Preferably, in step d, the phase state of the filler slurry can be determined by the CO2 injection pressure and flow rate, and when the CO2 injection pressure increases sharply and the flow rate is constant, the filler slurry is determined to be consolidated, and the CO2 injection can be stopped.|[0020] Preferably, the additive comprises fly ash, quicklime and magnesium slag powder for increasing carbon sequestration.|[0021] The invention also aims at providing a system based on a coordinated carbon dioxide sealing method for the fluidization, filling and disposal of mine solid wastes, in particular to a ground carbon fixing-ground well filling-underground carbon fixing system, which is arranged near a ground gangue mountain corresponding to the middle part of a mining area and comprises a feeder, a stirring carbon fixing reaction device, a filling pump and a filling pipeline which are connected in sequence; the feeder is respectively connected with a grinding workshop, a water tank and various additive material warehouses; the crushing workshop is connected with the grinding workshop;|[0022] The filling pipeline penetrates into the underground mining space, and the filling pipeline is provided with a filling pump; the filling pump is drilled beside the filling pump to the underground mining space, and the filling pipeline and the gas pipeline are arranged in the well; the CO2 gas source is connected with the gas pipeline, and the gas pipeline is divided into two sections of pipeline, one section of pipeline is connected with a stirring carbon fixing reaction device, and the other end of pipeline penetrates into the underground mining space.|[0023] The invention has the advantages that:|[0024] 1. The invention fills the mined-out area formed after the mining of coal resources with the solid waste base filling slurry of the mine with the function of mineralizing and sealing CO2, disposes the solid waste of the gangue mine piled up on the ground and the CO2 on a large scale, reduces the environmental damage caused by the solid waste ground piled up, realizes the green mining of coal resources and effectively protects the ecological environment of the mining area;|[0025] 2. In the method, waste fixation and CO2 storage are performed by forming a ground carbon fixation-ground well filling-downhole carbon fixation system, and CO2 gas is moved upward from the bottom of the filling slurry by ground carbon fixation, so as to increase the contact time and area between CO2 and the filling slurry. The mineralization of CO2 and the filling slurry fully reacts to realize the first CO2 sequestration; the underground carbon sequestration injects CO2 into the filling slurry to solidify the CO2, and simultaneously utilizes the porous adsorption property and the geological sealing property after the filling slurry solidifies, the mineralization sequestration and the physical sequestration to realize the second sequestration of CO2, the method of CO2 sequestration and the mine solid waste disposal amount are large, safe, efficient, practical and feasible, the cost is low, and the method has good popularization and application prospect.|Illustration Notes|[0026] In order to illustrate the embodiment of the invention or the technical solution of the prior art more clearly, the following is a brief introduction to the appended drawings needed in the embodiment or the description of the prior art. Obviously, the appended drawings described below are only some embodiments of the invention, and other appended drawings can be obtained according to the appended drawings without any creative work for ordinary technicians in the art;|[0027] FIG. 1 is a schematic diagram of a synergistic CO2 sequestration method for mine solid waste fluidization, filling and disposal provided in embodiment 1 of the present invention;|[0028] Illustration Mark-up Description:|[0029] In the picture: 1-ground gangue mountain; 2-crushing workshop; 3-grinding workshop; 4-each additive material bin; 5-water bin; 6-feeder; 7-stirring carbon fixation reaction device; 8-CO2 gas source; 9-filling pump; 10-filling pipeline; 11-underground mining space; 12-filling slurry; 13-gas pipeline.|Specific Implementation Methods|[0030] In that follow, the technical solution in the embodiment of the present invention will be clearly and completely describe in combination with the drawings in the embodiment of the present invention, and it is clear that the described embodiment is only one part of the embodiment of the present invention, and not all of the embodiments. Technologies, methods and equipment known to persons skilled in the art may not be discussed in detail, but where appropriate, such technologies, methods and equipment shall be deemed to be part of the Description of Authorization.|[0031] The invention discloses a collaborative carbon dioxide sealing method for fluidizing, filling and disposing solid wastes in a mine, which is characterized in that a mine solid waste base filling slurry 12 with the function of mineralizing and sealing CO2 is filled in a goaf formed after the mining of coal resources, thereby forming a ground carbon fixing-ground well filling-downhole carbon fixing system, and realizing the solid wastes disposal and the CO2 sealing. The invention is divided into three steps of ground carbon fixation, ground well filling and underground carbon fixation.|[0032] The invention firstly completes the ground carbon fixing process. After the solid waste of a mine such as coal gangue is crushed and ground, the coal gangue is mixed with additives such as fly ash, quicklime and magnesium slag powder according to a certain proportion, the mixed mass ratio of the coal gangue and the additives is 12 to 16:1, and the coal gangue is transported to a stirring carbon fixation reaction device 7; the coal gangue is crushed to meet the pumping requirement of filling slurry 12, and the particle diameter of the coal gangue is less than 10mm, wherein the proportion of the coal gangue is not less than 1/3 when the coal gangue is less than 2mm. in that agitation carbon fixation reaction device 7, a certain proportion of water is filled, 60 to 80% of coal gangue is added, the additive account for 5% of coal gangue, the rest is water, after continuous agitation, a CO2 gas source 8 is open at the same time, and a certain concentration of CO2 is continuously injected from the bottom of the agitation carbon fixation reaction device 7, The CO2 gas is moved upward from the bottom of the filling slurry 12 to increase the contact time and area of the CO2 and the filling slurry 12, so that the CO2 and the filling slurry 12 are fully reacted and mineralized, and the carbon fixing effect of the filling slurry 12 is realized, and the carbon fixing process on the ground is completed. The agitation reaction time of CO2 in that agitation carbon fixation reaction device 7 and the filling slurry 12 is determine according to the flow performance of the filling slurry and monitored by an automatic viscosity measuring instrument.|[0033] Preferably, to increase the carbon sequestration effect, the additive may preferably be magnesium slag powder and quicklime powder. The reaction equation of CO2 with CO2 is MgO+H2O→Mg(OH)2      (1)Mg(OH)2+CO2→MgCO3       (2) CaO+CO2→CaCO3             (3)|[0034] The invention then carries out the ground well filling process. First, the underground mining space 11 is accurately positioned, a ground-well drilling hole is arranged at the middle position of the underground mining space 11, and a filling pipeline 10 and a gas pipeline 13 are arranged in the ground-well drilling hole. The filling slurry 12 after fully reacting with CO2 is fed to the underground mining space 11 by the ground-well drilling pump through the filling pump 9 and the filling pipeline 10, and the ground well filling process is completed.|[0035] Finally, the invention carries out the downhole carbon fixation process. After the filling slurry 12 is filled with the underground mining space 11, the gas pipeline 13 is used to continuously inject CO2 into the inner part of the filling slurry 12 until the filling slurry 12 is solidified, and the phase state of the filling slurry can be determined by the injection pressure and the flow rate of the CO2; when the injection pressure of the CO2 increases rapidly and the flow rate is unchanged, the filling slurry 12 is determined to be solidified and the injection of the CO2 can be stopped. The porous adsorptive property and the geological sealing property of the packed slurry 12 after solidification are mainly used to seal the CO2 in the downhole carbon sequestration process. At this point, the downhole carbon sequestration process is completed, and finally the solid waste disposal and CO2 storage are realized.|[0036] Example 1|[0037] According to the description of the invention and in combination with the geological conditions of a coal mine engineering, an embodiment is described. The mining area of the mine has been mined, and the invention is implemented for all the mining spaces after the mining of the mining area is finished.|[0038] As shown in Figure 1, firstly, basic filling facilities are arranged near the ground gangue mountain 1 corresponding to the middle part of the mining area, including a crushing workshop 2, a grinding workshop 3, each additive material bin 4, a water bin 5, a feeder 6, a stirring carbon fixation reaction device 7, a CO2 gas source 8 and a filling pump 9. The feeding machine 6 is respectively connected with the grinding workshop 3, the water bin 5 and the additive material bin 4; the crushing workshop 2 is connected with the grinding workshop 3; solid wastes such as coal gangue are smashed by the crushing workshop 2 and input into the grinding workshop 3 for grinding; then the gangue, the additive materials and water are conveyed to the carbon-fixing reaction device 7 for mixing and stirring by the feeding machine 6 according to the proportion.|[0039] A filling pipeline 10 and a gas pipeline 13 are arranged in the well. The CO2 gas source 8 is connected with a gas pipeline 13, and the gas pipeline 13 is divided into two sections when passing through the stirring carbon fixation reaction device 7, one section is led into the stirring carbon fixation reaction device 7, and the other end is deep into the underground mining space 11.|[0040] The specific steps of the solid waste fluidization filling and disposal of the mine in cooperation with the carbon dioxide sealing are as follows:|[0041] a. Preparation procedures of filling materials: after the above-mentioned basic preparation work is completed, the preparation procedures of filling materials are started, first, coal gangue is crushed to a particle size of less than 10mm in a crushing workshop and a grinding workshop, and the proportion of less than 2 mm is not less than 1/3, and then the crushed and ground 70kg coal gangue is mixed with 3.5kg of lime and magnesium slag powder in each additive material bin and transported to a stirring carbon-fixing reaction device 7;|[0042] b. The ground carbon fixation process: Next, a first step carbon fixation process is carried out in a stirring carbon fixation reaction device 7, first, 26.5kg of water is added to the stirring carbon fixation reaction device 7, stirring is started, and CO2 gas is injected from the bottom of the stirring carbon fixation reaction device 7 through a CO2 gas source 8, and stirring can be stopped and CO2 injection can be stopped after the flow performance of the filling slurry reaches the minimum required by pumping.|[0043] c. Fluidization filling procedure: next, the fluidization filling procedure is started, the power is provided by the filling pump 9, and the stirred filling slurry 12 is transported to the underground mining space 11 through the filling pipeline 10;|[0044] d. Underground carbon sequestration process: after filling the filling slurry 12 to fill the underground mining space 11, opening the CO2 ground-well injection system, injecting CO2 into the interior of the underground filling slurry 12 through the gas pipeline 13, and when the injection pressure of the CO2 increases sharply and the flow rate remains unchanged, determining that the filling slurry 12 has solidified, so as to realize the fluid solid waste filling treatment and the CO2 sealing of the underground mining space 11 in the mining area.|[0045] It is clear that those skil in that art may make various modification and variations to the invention without departing from the spirit and scope of the invention. In this way, if these modification and variants of that invention are within the scope of the claims of the invention and their equivalent techniques, the invention also intends to include these modification and variants. (WO2024/082838)|technical field|[0001] The invention relates to the field of coal mine green mining and carbon storage, in particular to a synergistic carbon dioxide storage method for solid waste fluidization, filling and treatment in a mine.|background technology|[0002] China's coal-rich, lean-oil and gas-poor energy characteristics determine the status of China's main energy. As the associated solid waste in coal mining, coal gangue usually discharges and deposits on the ground, accounting for 20% of the coal output. It not only occupies a large number of scarce land resources, causing a huge impact on the ecological environment of the mining area, but also will bring a series of potential safety hazards such as gangue mountain spontaneous combustion. In the face of the pressure of ecological environment protection, how to deal with solid waste such as coal gangue efficiently is one of the problems faced by the high quality development of coal enterprises.|[0003] On the other hand, climate change is a global problem facing mankind, CO2 emissions are increasing, and it is a threat to life systems. Developing CO2 capture, utilization and storage (CCUS) technology is not only a strategic choice for reducing CO2 emissions and ensuring energy security in the future, but also an important means for constructing ecological civilization and achieving sustainable development. CO2 sequestration is the process of CO2 capture into deep geological reservoir by engineering technology and realize long-term isolation of CO2 from the atmosphere.|[0004] At present, the key technology of using coal gangue, tailings and other materials for mineralization and carbon dioxide adsorption is mainly concentrated in the addition of effective additives, but this kind of method can only consume a small amount of coal gangue or end the CO2 sequestration process of waste coal gangue difficult to be reasonably disposed. For example, "a system for removing flue gas CO2 from a power plant by using a modified coal gangue and an implementation method thereof" uses an organic amine active component to spray and load on the modified broken coal gangue to capture CO2, the CO2 capture effect is good, but the CO22 finally used as a carrier is still difficult to be reasonably disposed.|[0005] But the technology which is related to underground treatment of coal gangue and synchronous sequestration often transport the filling material to the underground and then carry out the carbon injection and other processes and lose the advantages of mineralization in the well, or is limited by the storage space and can only achieve a small storage. For example, the system and method for "short-long-wall intermittent filling and mining synergistic alkali-based solid CO2 storage" fill the prepared filling material into the short-wall working surface of the well and then carry out carbon filling and storage, and discard the advantage conditions of full mineralization of auxiliary filling material of large-scale equipment on the well; for example, "a method for waste treatment and carbon dioxide storage of coal-fired power plants at the pit" adopts gangue, cement and alkaline aqueous solution to directly capture the CO2 of the power plant and then fill the waste wellbore, the filling space and the storage amount of which are limited by the capacity of the waste wellbore.|[0006] Therefore, the prior art has the advantages that the amount of the coal gangue consumed in the well sealing is small, the waste such as the coal gangue can not be reasonably treated after the well sealing is carried out, the auxiliary filling material of the large-scale equipment in the well is fully mineralized after the well sealing is discarded in the well sealing, and the well sealing is limited by the sealing space, so that the small sealing amount can only be realized.|[0007] Contents of Invention|[0008] The invention aims at providing a synergistic carbon dioxide sealing method for the fluidization, filling and disposal of solid waste in mines, which sequentially forms a ground carbon fixing-ground well filling-underground carbon fixing system based on the mineralization characteristics of the solid waste of coal gangue and CO2, prepares a filling slurry with coal gangue and additives, fully mixes and stirs the slurry with CO2, and then fills the underground extraction space and fills the CO2, This method is safe, efficient, practical, and low-cost. It can realize green mining of coal resources and underground space CO2 storage, reducing the damage to the ecological environment caused by coal mining, and has a broad application prospect.|[0009] At present, the use of CO2 mineralization principle is one of the main ways to achieve CO2 geological storage, that is, CO2 and rock occurred a rapid chemical reaction and formed a new carbonate minerals, through this method, CO2 was permanently "confined" in the rock, achieved CO2 mineralized geological storage.|[0010] The inventor discovers that the calcium magnesium compounds contained in solid wastes such as coal gangue can react with CO2 to form carbonate minerals, and therefore proposes a collaborative carbon dioxide sealing method for the fluidization, filling and disposal of solid wastes in mines, and the coal gangue solid wastes and the CO2 are simultaneously disposed and sealed in the coal mining space, which is of great significance for reducing the damage to the environment caused by coal mining and reducing the greenhouse gas emission, and conforms to the strategic goal of "double carbon" in China.|[0011] In order to realize the above-mentioned purpose, the invention adopts the following technical proposal:|[0012] The invention aims at a collaborative carbon dioxide sealing method for the fluidization, filling and disposal of solid wastes in a mine, which is based on the mineralization characteristics of gangue solid wastes and CO2, sequentially forms a ground carbon fixing, ground well filling and underground carbon fixing system, and fills a mined area formed after the mining of coal resources with a mine solid waste base filling slurry with the function of mineralization and sealing CO2, thus realizing the solid wastes disposal and the sealing of CO2 in a mine, and specifically comprises the following steps:|[0013] a. Preparation of filling materials: firstly, the coal gangue is crushed in a crushing workshop and a grinding workshop, and then the crushed and ground coal gangue is mixed with the additives in each additive material bin and transported to a stirring carbon fixation reaction device;|[0014] b. The process of carbon fixation on the ground: adding a certain amount of water to the stirring carbon fixation reaction device, starting stirring, and starting to inject CO2 gas from the bottom of the stirring carbon fixation reaction device through a CO2 gas source, and stopping stirring and stopping injecting CO2 after the flow performance of the filling slurry reaches the minimum required by pumping;|[0015] (c) Fluidization filling process: a filling pump is used to provide power, and the agitated filling slurry is transported to the underground mining space through a filling pipeline of a ground-well drilling hole;|[0016] d. Underground carbon sequestration working procedure: after the filling slurry fills the underground mining space, the CO2 ground-well injection system is opened, and the CO2 is injected into the inner part of the underground filling slurry through a gas pipeline until the filling slurry is consolidated, thereby realizing the fluidization solid waste filling treatment and the CO2 sealing of the underground mining space in the mining area.|[0017] Preferably, in step b, the coal gangue crushing needs to meet the pumping requirement of the filling slurry, the coal gangue particle size is less than 10mm, and the proportion of the coal gangue particle size less than 2 mm is not less than 1/3.|[0018] Preferably, in step b, the agitation reaction time of CO2 with the filler slurry in the agitation carbon fixation reaction apparatus is determined according to the flow performance of the filler slurry and monitored by a viscosity automatic meter.|[0019] Preferably, in step d, the phase state of the filler slurry can be determined by the CO2 injection pressure and flow rate, and when the CO2 injection pressure increases sharply and the flow rate is constant, the filler slurry is determined to be consolidated, and the CO2 injection can be stopped.|[0020] Preferably, the additive comprises fly ash, quicklime and magnesium slag powder for increasing carbon sequestration.|[0021] The invention also aims at providing a system based on a coordinated carbon dioxide sealing method for the fluidization, filling and disposal of mine solid wastes, in particular to a ground carbon fixing-ground well filling-underground carbon fixing system, which is arranged near a ground gangue mountain corresponding to the middle part of a mining area and comprises a feeder, a stirring carbon fixing reaction device, a filling pump and a filling pipeline which are connected in sequence; the feeder is respectively connected with a grinding workshop, a water tank and various additive material warehouses; the crushing workshop is connected with the grinding workshop;|[0022] The filling pipeline penetrates into the underground mining space, and the filling pipeline is provided with a filling pump; the filling pump is drilled beside the filling pump to the underground mining space, and the filling pipeline and the gas pipeline are arranged in the well; the CO2 gas source is connected with the gas pipeline, and the gas pipeline is divided into two sections of pipeline, one section of pipeline is connected with a stirring carbon fixing reaction device, and the other end of pipeline penetrates into the underground mining space.|[0023] The invention has the advantages that:|[0024] 1. The invention fills the mined-out area formed after the mining of coal resources with the solid waste base filling slurry of the mine with the function of mineralizing and sealing CO2, disposes the solid waste of the gangue mine piled up on the ground and the CO2 on a large scale, reduces the environmental damage caused by the solid waste ground piled up, realizes the green mining of coal resources and effectively protects the ecological environment of the mining area;|[0025] 2. In the method, waste fixation and CO2 storage are performed by forming a ground carbon fixation-ground well filling-downhole carbon fixation system, and CO2 gas is moved upward from the bottom of the filling slurry by ground carbon fixation, so as to increase the contact time and area between CO2 and the filling slurry. The mineralization of CO2 and the filling slurry fully reacts to realize the first CO2 sequestration; the underground carbon sequestration injects CO2 into the filling slurry to solidify the CO2, and simultaneously utilizes the porous adsorption property and the geological sealing property after the filling slurry solidifies, the mineralization sequestration and the physical sequestration to realize the second sequestration of CO2, the method of CO2 sequestration and the mine solid waste disposal amount are large, safe, efficient, practical and feasible, the cost is low, and the method has good popularization and application prospect.|Illustration Notes|[0026] In order to illustrate the embodiment of the invention or the technical solution of the prior art more clearly, the following is a brief introduction to the appended drawings needed in the embodiment or the description of the prior art. Obviously, the appended drawings described below are only some embodiments of the invention, and other appended drawings can be obtained according to the appended drawings without any creative work for ordinary technicians in the art;|[0027] FIG. 1 is a schematic diagram of a synergistic CO2 sequestration method for mine solid waste fluidization, filling and disposal provided in embodiment 1 of the present invention;|[0028] Illustration Mark-up Description:|[0029] In the picture: 1-ground gangue mountain; 2-crushing workshop; 3-grinding workshop; 4-each additive material bin; 5-water bin; 6-feeder; 7-stirring carbon fixation reaction device; 8-CO2 gas source; 9-filling pump; 10-filling pipeline; 11-underground mining space; 12-filling slurry; 13-gas pipeline.|Specific Implementation Methods|[0030] In that follow, the technical solution in the embodiment of the present invention will be clearly and completely describe in combination with the drawings in the embodiment of the present invention, and it is clear that the described embodiment is only one part of the embodiment of the present invention, and not all of the embodiments. Technologies, methods and equipment known to persons skilled in the art may not be discussed in detail, but where appropriate, such technologies, methods and equipment shall be deemed to be part of the Description of Authorization.|[0031] The invention discloses a collaborative carbon dioxide sealing method for fluidizing, filling and disposing solid wastes in a mine, which is characterized in that a mine solid waste base filling slurry 12 with the function of mineralizing and sealing CO2 is filled in a goaf formed after the mining of coal resources, thereby forming a ground carbon fixing-ground well filling-downhole carbon fixing system, and realizing the solid wastes disposal and the CO2 sealing. The invention is divided into three steps of ground carbon fixation, ground well filling and underground carbon fixation.|[0032] The invention firstly completes the ground carbon fixing process. After the solid waste of a mine such as coal gangue is crushed and ground, the coal gangue is mixed with additives such as fly ash, quicklime and magnesium slag powder according to a certain proportion, the mixed mass ratio of the coal gangue and the additives is 12 to 16:1, and the coal gangue is transported to a stirring carbon fixation reaction device 7; the coal gangue is crushed to meet the pumping requirement of filling slurry 12, and the particle diameter of the coal gangue is less than 10mm, wherein the proportion of the coal gangue is not less than 1/3 when the coal gangue is less than 2mm. in that agitation carbon fixation reaction device 7, a certain proportion of water is filled, 60 to 80% of coal gangue is added, the additive account for 5% of coal gangue, the rest is water, after continuous agitation, a CO2 gas source 8 is open at the same time, and a certain concentration of CO2 is continuously injected from the bottom of the agitation carbon fixation reaction device 7, The CO2 gas is moved upward from the bottom of the filling slurry 12 to increase the contact time and area of the CO2 and the filling slurry 12, so that the CO2 and the filling slurry 12 are fully reacted and mineralized, and the carbon fixing effect of the filling slurry 12 is realized, and the carbon fixing process on the ground is completed. The agitation reaction time of CO2 in that agitation carbon fixation reaction device 7 and the filling slurry 12 is determine according to the flow performance of the filling slurry and monitored by an automatic viscosity measuring instrument.|[0033] Preferably, to increase the carbon sequestration effect, the additive may preferably be magnesium slag powder and quicklime powder. The reaction equation of CO2 with CO2 is MgO+H2O→Mg(OH)2      (1)Mg(OH)2+CO2→MgCO3       (2) CaO+CO2→CaCO3             (3)|[0034] The invention then carries out the ground well filling process. First, the underground mining space 11 is accurately positioned, a ground-well drilling hole is arranged at the middle position of the underground mining space 11, and a filling pipeline 10 and a gas pipeline 13 are arranged in the ground-well drilling hole. The filling slurry 12 after fully reacting with CO2 is fed to the underground mining space 11 by the ground-well drilling pump through the filling pump 9 and the filling pipeline 10, and the ground well filling process is completed.|[0035] Finally, the invention carries out the downhole carbon fixation process. After the filling slurry 12 is filled with the underground mining space 11, the gas pipeline 13 is used to continuously inject CO2 into the inner part of the filling slurry 12 until the filling slurry 12 is solidified, and the phase state of the filling slurry can be determined by the injection pressure and the flow rate of the CO2; when the injection pressure of the CO2 increases rapidly and the flow rate is unchanged, the filling slurry 12 is determined to be solidified and the injection of the CO2 can be stopped. The porous adsorptive property and the geological sealing property of the packed slurry 12 after solidification are mainly used to seal the CO2 in the downhole carbon sequestration process. At this point, the downhole carbon sequestration process is completed, and finally the solid waste disposal and CO2 storage are realized.|[0036] Example 1|[0037] According to the description of the invention and in combination with the geological conditions of a coal mine engineering, an embodiment is described. The mining area of the mine has been mined, and the invention is implemented for all the mining spaces after the mining of the mining area is finished.|[0038] As shown in Figure 1, firstly, basic filling facilities are arranged near the ground gangue mountain 1 corresponding to the middle part of the mining area, including a crushing workshop 2, a grinding workshop 3, each additive material bin 4, a water bin 5, a feeder 6, a stirring carbon fixation reaction device 7, a CO2 gas source 8 and a filling pump 9. The feeding machine 6 is respectively connected with the grinding workshop 3, the water bin 5 and the additive material bin 4; the crushing workshop 2 is connected with the grinding workshop 3; solid wastes such as coal gangue are smashed by the crushing workshop 2 and input into the grinding workshop 3 for grinding; then the gangue, the additive materials and water are conveyed to the carbon-fixing reaction device 7 for mixing and stirring by the feeding machine 6 according to the proportion.|[0039] A filling pipeline 10 and a gas pipeline 13 are arranged in the well. The CO2 gas source 8 is connected with a gas pipeline 13, and the gas pipeline 13 is divided into two sections when passing through the stirring carbon fixation reaction device 7, one section is led into the stirring carbon fixation reaction device 7, and the other end is deep into the underground mining space 11.|[0040] The specific steps of the solid waste fluidization filling and disposal of the mine in cooperation with the carbon dioxide sealing are as follows:|[0041] a. Preparation procedures of filling materials: after the above-mentioned basic preparation work is completed, the preparation procedures of filling materials are started, first, coal gangue is crushed to a particle size of less than 10mm in a crushing workshop and a grinding workshop, and the proportion of less than 2 mm is not less than 1/3, and then the crushed and ground 70kg coal gangue is mixed with 3.5kg of lime and magnesium slag powder in each additive material bin and transported to a stirring carbon-fixing reaction device 7;|[0042] b. The ground carbon fixation process: Next, a first step carbon fixation process is carried out in a stirring carbon fixation reaction device 7, first, 26.5kg of water is added to the stirring carbon fixation reaction device 7, stirring is started, and CO2 gas is injected from the bottom of the stirring carbon fixation reaction device 7 through a CO2 gas source 8, and stirring can be stopped and CO2 injection can be stopped after the flow performance of the filling slurry reaches the minimum required by pumping.|[0043] c. Fluidization filling procedure: next, the fluidization filling procedure is started, the power is provided by the filling pump 9, and the stirred filling slurry 12 is transported to the underground mining space 11 through the filling pipeline 10;|[0044] d. Underground carbon sequestration process: after filling the filling slurry 12 to fill the underground mining space 11, opening the CO2 ground-well injection system, injecting CO2 into the interior of the underground filling slurry 12 through the gas pipeline 13, and when the injection pressure of the CO2 increases sharply and the flow rate remains unchanged, determining that the filling slurry 12 has solidified, so as to realize the fluid solid waste filling treatment and the CO2 sealing of the underground mining space 11 in the mining area.|[0045] It is clear that those skil in that art may make various modification and variations to the invention without departing from the spirit and scope of the invention. In this way, if these modification and variants of that invention are within the scope of the claims of the invention and their equivalent techniques, the invention also intends to include these modification and variants. Family Number|(103532840)|103532840|Abstract|(CN115628106B B)|The invention relates to a mine solid waste fluidized filling treatment and carbon dioxide sealing method , which comprises the following steps : forming a ground carbon sequestration - ground well filling - underground carbon sequestration system , filling mine solid waste - based filling slurry with a mineralization CO2 sealing function into a goaf formed after coal resources are mined , and realizing mine solid waste treatment and CO2 sealing . The method specifically comprises the following steps : mixing crushed coal gangue and an additive , conveying the mixture to a stirring carbon sequestration reaction device , adding water into the stirring carbon sequestration reaction device , stirring , injecting CO2 gas from the bottom , and stopping injecting CO2 after the flowing property of slurry reaches the minimum limit required by pumping ; and the filling pump conveys the slurry to the underground extraction space through the filling pipeline , and after the underground extraction space is filled with the slurry , CO2 is injected into the underground slurry through the gas pipeline until the slurry is solidified . The method is safe , efficient , practicable and low in cost , green mining of coal resources and underground space CO2 storage are achieved , and damage of coal mining to the ecological environment is reduced . |(WO202482838 A1)|Disclosed are a method for synergistic fluidization filling disposal of solid mine waste and carbon dioxide storage and a system based on the method. In the method, a ground carbon sequestration-ground well filling-downhole carbon sequestration system is formed, and a solid mine waste-based filling slurry (12) with a CO2 mineralization storage function is introduced into a goaf which is formed after coal resources are mined, thereby realizing the disposal of solid mine waste and CO2 storage. The method specifically comprises: mixing crushed coal gangue with an additive, conveying the mixture to a stirring carbon sequestration reaction device (7), adding water thereto and stirring same, injecting CO2 gas into same from the bottom, and stopping injecting CO2 after the flowing performance of the slurry reaches the minimum limit required by pumping; conveying the filling slurry to a downhole goaf (11) by means of a filling pump (9) via a filling pipeline (10); and after the downhole goaf is filled with the filling slurry, injecting CO2 into the downhole slurry via a gas pipeline (13) until the slurry is solidified. The method is safe, efficient and feasible, has low costs, achieves green mining of coal resources and CO2 storage in a downhole space, and reduces the damage of coal mining to the ecological environment.|CPC codes|(CN115628106B B)|B01D - 053/62 |B01D - 053/80 |(WO202482838 A1)|B01D-053/62|B01D-053/80|IPC codes|(CN115628106B B)|B01D - 053/62 |B01D - 053/80 |(WO202482838 A1)|B01D-053/62|B01D-053/80| Civil engineering|Environmental technology B01D-053/62|B01D-053/80|E21F-015/00/5|E21F-015/06|Y02C-020/40 B01D-053/62|B01D-053/80|E21F-015/00/5|E21F-015/06|Y02C-020/40 B01D-053/62|B01D-053/80|E21F-015/00|E21F-015/06 B01D-053/62|B01D-053/80|E21F-015/00|E21F-015/06 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76763608 WHO=Examiner SELF=N CAT=A|US20140056646 61860030 WHO=Examiner SELF=N CAT=A|WO201147070 44619241 WHO=Examiner SELF=N CAT=A|EP1801346 14891115 WHO=Examiner SELF=N CAT=A CN114673552; CN115628106; CN115095387; CN113339056; CN113101789; CN114956750; CN114856689; WO201147070; EP1801346|US20140056646; CN106946255; CN107762554; CN113101789; CN113213829; CN113339056; CN114673552; CN114956750 GRANTED (WO2024/082838)|LAPSED|(CN115628106)|GRANTED ALIVE (WO2024/082838)|DEAD|(CN115628106)|ALIVE (WO2024/082838)|LEGAL DETAILS FOR WO2024/082838|Actual or expected expiration date=2026-04-18|Legal state=DEAD|Status=LAPSED|Event publication date=2023-09-04|Event code=WO/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=WO WOCN2023/116687|Application date=2023-09-04|Standardized application number=2023WO-CN116687|Event publication date=2024-04-25|Event code=WO/A1|Event group=Examination events|Published application with search report|Publication 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AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (CN115628106)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCCU4RAtukjamonVC+dywuLYbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006468622&ekey=2292&xpn=WO202482838&kind=A1 http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2024082838&redirectedID=true https://permalink.orbit.com/RenderStaticFirstPage?XPN=9OS%252Bjxzgn5NpjSuNKPoRzZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (WO2024/082838)|CN|(CN115628106)|CN|(CN115628106)|CN (WO2024/082838)|NAME=CHINA UNIVERSITY OF MINING AND TECHNOLOGY No. 1, Daxue Road, Tongshan Xuzhou, Jiangsu 221116 , COUNTRY=CN|(CN115628106)|NAME=CHINA UNIVERSITY OF MINING & TECHNOLOGY , COUNTRY=CN|(CN115628106)|NAME=CHINA UNIVERSITY OF MINING & TECHNOLOGY , COUNTRY=CN (WO2024/082838)|CN|| (WO2024/082838)|NAME=NANJING JINGWEI PATENT & TRADEMARK AGENCY CO., LTD 12th FL.-B, No. 179 Zhongshan Road, Gulou Nanjing, Jiangsu 210005 , POSTCODE=210005 , COUNTRY=CN|(CN115628106)|NAME=GUO LINA;NANJING JINGWEI PATENT & TRADEMARK AGENCY CO., LTD , REG=32200|(CN115628106)|NAME=GUO LINA;NANJING JINGWEI PATENT & TRADEMARK AGENCY CO., LTD , REG=32200 (WO2024/082838)|CN; CN; CN; CN; CN; CN|| (WO2024/082838)|NAME=LI, Baiyi No. 1, Daxue Road, Tongshan Xuzhou, Jiangsu 221116, POSTCODE=221116, COUNTRY=CN |NAME=LONG, Kang No. 1, Daxue Road, Tongshan Xuzhou, Jiangsu 221116, POSTCODE=221116, COUNTRY=CN |NAME=GUO, Yuming No. 1, Daxue Road, Tongshan Xuzhou, Jiangsu 221116, POSTCODE=221116, COUNTRY=CN |NAME=ZHANG, Jixiong No. 1, Daxue Road, Tongshan Xuzhou, Jiangsu 221116, POSTCODE=221116, COUNTRY=CN |NAME=MA, Jiayuan No. 1, Daxue Road, Tongshan Xuzhou, Jiangsu 221116, POSTCODE=221116, COUNTRY=CN |NAME=ZHOU, Nan No. 1, Daxue Road, Tongshan Xuzhou, Jiangsu 221116, POSTCODE=221116, COUNTRY=CN|(CN115628106)|NAME=LI BAIYI|NAME=GUO YUMING|NAME=ZHANG JIXIONG|NAME=GAO FENG|NAME=MA JIAYUAN|NAME=ZHOU NAN|(CN115628106)|NAME=LI BAIYI|NAME=GUO YUMING|NAME=ZHANG JIXIONG|NAME=GAO FENG|NAME=MA JIAYUAN|NAME=ZHOU NAN 11 2 Titre: (WO2024/082838)|Method for synergistic fluidization filling disposal of solid mine waste and carbon dioxide storage Résumé: (WO2024/082838)|Disclosed are a method for synergistic fluidization filling disposal of solid mine waste and carbon dioxide storage and a system based on the method. In the method, a ground carbon sequestration-ground well filling-downhole carbon sequestration system is formed, and a solid mine waste-based filling slurry (12) with a CO2 mineralization storage function is introduced into a goaf which is formed after coal resources are mined, thereby realizing the disposal of solid mine waste and CO2 storage. The method specifically comprises: mixing crushed coal gangue with an additive, conveying the mixture to a stirring carbon sequestration reaction device (7), adding water thereto and stirring same, injecting CO2 gas into same from the bottom, and stopping injecting CO2 after the flowing performance of the slurry reaches the minimum limit required by pumping; conveying the filling slurry to a downhole goaf (11) by means of a filling pump (9) via a filling pipeline (10); and after the downhole goaf is filled with the filling slurry, injecting CO2 into the downhole slurry via a gas pipeline (13) until the slurry is solidified. The method is safe, efficient and feasible, has low costs, achieves green mining of coal resources and CO2 storage in a downhole space, and reduces the damage of coal mining to the ecological environment. 105 Abstract gpt-4o-mini no The focus is on the disposal of solid mine waste and CO2 storage in a downhole space, rather than on the accelerated weathering of minerals for carbon sequestration.
103 CN202310205820 CN202310205820 CN116832605|CN116832605 106744235 CN116832605 B 2026-04-14 [CN116832605B]|CN116832605 A 2023-10-03 [CN116832605] 2023-03-06 2023-03-06 2026-04-14|2023-10-03 (CN116832605B)|2026-04-14 (CN116832605)|2043-03-06 (CN116832605)|Method for functionally utilizing smoke catcher of coal-fired power plant (CN116832605)|The invention relates to the technical field of carbon dioxide sequestration and water purification, in particular to a method for functionalized utilization of flue gas traps of a coal-fired power plant, and discloses the method for functionalized utilization of the flue gas traps of the coal-fired power plant, which comprises the following steps: taking steel slag as a raw material, performing primary grinding on blocky steel slag to obtain steel slag coarse powder, performing secondary grinding, and performing secondary grinding to obtain the flue gas traps of the coal-fired power plant. Steel slag micro powder is obtained; 20-50 parts by weight of steel slag micro powder and 1-5 parts by weight of ammonium salt are evenly mixed, a mixture is obtained, and water is added. According to the method for functionalized utilization of the flue gas traps of the coal-fired power plant, steel slag is used as a main raw material and cooperates with ammonium salt liquid-phase grinding, coal-fired flue gas is introduced, on one hand, steel slag particles are fully crushed through liquid-phase grinding, the contact area of CO2 in the coal-fired flue gas and the steel slag is increased while calcium ion dissolution is promoted, on the other hand, CO2 dissolution can be promoted through cooperation with ammonium salt grinding, and the CO2 content in the coal-fired flue gas is increased. Meanwhile, the steel slag carbon sequestration efficiency is improved. HUBEI UNIVERSITY OF TECHNOLOGY (CN116832605)|HUBEI UNIVERSITY OF TECHNOLOGY ([CN])|(CN116832605)|HUBEI UNIVERSITY OF TECHNOLOGY ([CN]) HE XINGYANG|XIAO HUCHENG|YANG JIN|SU YING|DAI FEI|WANG YINGBIN|LIU SENYE|ZHANG JUNHUN|WANG ZHIRUI (CN116832605)|HE XINGYANG|XIAO HUCHENG|YANG JIN|SU YING|DAI FEI|WANG YINGBIN|LIU SENYE|ZHANG JUNHUN|WANG ZHIRUI|(CN116832605)|HE XINGYANG|XIAO HUCHENG|YANG JIN|SU YING|DAI FEI|WANG YINGBIN|LIU SENYE|ZHANG JUNHUN|WANG ZHIRUI (CN116832605)|QIAN CHUNHU;WUHAN SINOPOWER PATENT AGENCY|Reg. Nb: 42237 (CN116832605)|Aiming at the defects of the prior art, the invention provides a method for functionally utilizing the coal-fired power plant flue gas catcher, which has the advantages of high value-added utilization of steel slag and the like, and solves the problem of low value-added utilization of the existing steel slag.|At present, the domestic steel slag has lower additional value utilization, how to utilize the steel slag to seal and store CO _2 of the coal-fired power plant and realize the high additional value utilization of the steel slag, the permanent seal and the functional utilization of carbon-fixing products of CO _2 of the coal-fired power plant, and the aim of treating waste with waste and being environment-friendly is achieved, which is a problem to be solved by the current technicians in the field.|Therefore, the calcium element in the steel slag is difficult to dissolve in the water medium under mild environmental conditions, so that the mineralization efficiency is low.| (CN116832605)|1. The method for functionally utilizing the flue gas catcher of the coal-fired power plant is characterized by comprising the following steps of: 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; 2) Uniformly mixing 20-50 parts by weight of steel slag micro powder and 1-5 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be 12.5% -33.3% to obtain a mixed slurry A; 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, and introducing coal-fired flue gas to obtain a carbon-fixing functional admixture; 4) Uniformly mixing 20-40 parts by weight of carbon fixation function admixture, 40-80 parts by weight of cement, 30-55 parts by weight of fly ash and 7-15 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; 5) Starting a granulator, then slowly sprinkling water for 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting a spray head, slightly converging a streamline shape, and slowly spraying water by aiming at the edge part of the rolling material to prepare the carbon-fixing function baking-free ceramsite; the maximum particle size of the perlite particles is not higher than 2.63mm, and the particle size range of the fly ash is 0.5-300 mu m; The rotating speed of the circular pan granulator is 10-50 r/min, and the elevation angle of the circular pan granulator is 20-45 degrees; The median particle diameter of the steel slag micro powder is 40-60 mu m, the CaO content of the steel slag micro powder is not lower than 30%, and the Fe 2O3 content of the steel slag micro powder is not lower than 15%; The solid content represents the proportion of the mixture to water, and the ammonium salt is one of ammonium nitrate, ammonium chloride, ammonium acetate and ammonium sulfate; the dispersing agent is one of sodium dodecyl benzene sulfonate, sodium hexametaphosphate and polyethylene glycol, the pH value of the carbon fixing functional admixture is 7-8, the median particle diameter is 2-5 mu m, and the content of Fe (OH) 3 is not less than 15%; the sprinkling lasts for 0.5-2 s, each sprinkling interval is 5-10 s, one sprinkling lasts for 1-3 s, and each sprinkling interval is 7-15 s. | (CN116832605)|The invention provides a method for capturing flue gas of a coal-fired power plant and functionally utilizing captured products thereof.|The invention relates to the technical field of carbon dioxide sequestration and water purification, in particular to a method for functionally utilizing a flue gas catcher of a coal-fired power plant, and discloses a method for functionally utilizing the flue gas catcher of the coal-fired power plant.|The invention relates to the technical field of carbon dioxide sequestration and water purification, in particular to a method for functionally utilizing a flue gas collector of a coal-fired power plant.| (CN116832605)|CIRCULAR PAN GRANULATOR(100,14)|COAL FIRED POWER(100,1)|COAL FIRED POWER CATCHER(100,1)|STEEL SLAG(91,33)|FLUE GAS CATCHER(87,12)|SLAG COARSE POWDER(79,20)|STEEL SLAG MICRO POWDER(76,26)|SLAG MICRO POWDER(75,26)|STEEL SLAG COARSE POWDER(70,20)|PERLITE PARTICLE(62,13)|MASSIVE STEEL SLAG(56,10)|SODIUM DODECYL BENZENE SULFONATE(55,2)|SPRINKLER(51,2)|ADMIXTURE FUNCTION(50,24)|AVERAGE PARTICLE DIAMETER(47,11)|UTILIZATION FUNCTION(47,1)|CERAMSITE FINENESS MODULUS(46,3)|WASTE TREATMENT(44,1)|CARBON FIXING FUNCTIONAL ADMIXTURE(42,24)|CAO CONTENT(42,2)|PERMANENT SEAL(42,1)|TECHNICIAN(41,1)|FLUE GAS(40,32)|FE CONTENT(40,2)|STIRRING BALL MILL(40,2)|UTILIZING VALUE(39,2)|COAL FIRED FLUE GAS(38,16)|FLUE GAS CAPTURE(38,1)|STEEL SLAG VALUE UTILIZATION(37,1)|SPHERICAL PARTICLE(35,10)|FLUE GAS COLLECTOR(35,1)|STEEL SLAG PARTICLE(34,3)|CARBON DIOXIDE SEQUESTRATION(34,2)|CAPTURED PRODUCT(34,1)|DOMESTIC(34,1)|COAL FIRED POWER PLANT(33,18)|MINERALIZATION(32,4)|CATCHER(29,1)|MILD ENVIRONMENTAL CONDITION(29,1)|STIRRED BALL MILL(28,12)|ROTATING SPEED(28,3)|GRINDING(27,21)|SODIUM HEXAMETAPHOSPHATE(27,2)|FLY ASH(26,12)|GRANULATOR(26,10)|MIXED SLURRY(26,9)|BAKING FREE CERAMSITE(26,5)|AMMONIUM SALT GRINDING(26,2)|BALL PROPORTION(26,2)|STACKING DENSITY(26,2)|SOLID CONTENT(25,11)|ROLLING(25,10)|SPRAY HEAD(25,10)|WATER PURIFICATION(25,2)|DISPERSING AGENT(23,12)|AMMONIUM NITRATE(23,3)|AMMONIUM SALT(22,18)|ADMIXTURE(22,4)|POLYETHYLENE GLYCOL(21,2)|CARBON FIXATION(20,11)|CARBON FIXING(19,44)|SLURRY(19,9)|GAS VELOCITY(19,2)|SLAG(19,2)|SPRAYING(18,10)|AMMONIUM SULFATE(18,3)|AMMONIUM ACETATE(17,4)|AMMONIUM CHLORIDE(17,3)|ROLLING MATERIAL(16,10)|CARBON FIXING PRODUCT(16,2)|STEEL SLAG STRENGTHENING MINERALIZATION(15,1)|VALUE ADDED UTILIZATION(14,3)|ELEVATION ANGLE(14,2)|GRINDING LIQUID PHASE(14,2)|BAKING FREE CERAMIC PARTICLE(12,9)|R MIN(11,4)|MAXIMUM PARTICLE SIZE(11,2)|STEEL SLAG CA DISSOLUTION(11,1)|CALCIUM ION(10,3)|AUXILIARY ADDITIVE(10,2)|PARTICLE SIZE(10,2)|FRACTIONAL SCREEN RESIDUE CALCULATION(9,1)|STEEL SLAG ADSORPTION(9,1)|ADSORPTION EXPERIMENT(8,1)|CONTACT AREA(7,2)|ARSENIC ADSORPTION RATE(7,1)|CERAMSITE BASIC PERFORMANCE(7,1)|CERAMSITE PERFORMANCE(7,1)|SIEVE(6,6)|FUNCTIONAL BAKING FREE CERAMSITE(6,2)|POLYETHYLENE PLASTIC BOTTLE(6,2)|ADDITIVE FUNCTION(5,1)|ADSORPTION REACTION(5,1)|CARBON FIXING ADSORPTION(5,1)|CARBONIZATION REACTION(5,1)|STEEL SLAG CARBON FIXATION(5,1)|WET GRINDING(5,1)|ALKALINE SOLID WASTE(4,3)|ALKALINITY(4,1)|AUXILIARY MODE(4,1)|CA2FE2O(4,1)|CA3SIO(4,1)||(CN116832605)|FLUE GAS(100,40)|COAL FIRED POWER PLANT(100,25)|SLAG COARSE POWDER(100,22)|FLUE GAS CATCHER(100,11)|CATCHER(100,2)|STEEL SLAG COARSE POWDER(88,22)|STEEL SLAG(84,32)|STEEL SLAG MICRO POWDER(72,26)|SLAG MICRO POWDER(70,26)|MASSIVE STEEL SLAG(70,11)|CIRCULAR PAN GRANULATOR(69,14)|CARBON DIOXIDE SEQUESTRATION(59,2)|ADMIXTURE FUNCTION(55,28)|SPRINKLING INTERVAL(54,2)|FLUE GAS COLLECTOR(48,4)|PERLITE PARTICLE(46,13)|COLLECTOR(43,2)|CARBON FIXING FUNCTIONAL ADMIXTURE(40,25)|CERAMSITE FINENESS MODULUS(40,3)|UTILIZATION FUNCTION(40,1)|PERMANENT SEALING(39,1)|WASTE TREATMENT(38,1)|TECHNICIAN(35,1)|STIRRING BALL MILL(34,2)|COAL FIRED FLUE GAS(33,16)|CARBON FIXATION FUNCTIONAL ADMIXTURE(33,3)|SPHERICAL PARTICLE(30,10)|LIQUID PHASEGRINDING(30,1)|PRODUCT UTILIZATION FUNCTION(30,1)|CERAMIC PARTICLE(29,10)|MINERALIZATION(29,3)|STEEL SLAG PARTICLE(29,3)|FLUE GAS TRAP(29,2)|CAPTURED PRODUCT(29,1)|DOMESTIC(29,1)|GRINDING(27,23)|AMMONIUM SALT(25,8)|MILD ENVIRONMENTAL CONDITION(25,1)|UTILIZING VALUE(25,1)|STIRRED BALL MILL(24,12)|STEEL SLAG CARBON FIXATION(24,3)|BAKING FREE CERAMSITE(24,2)|GRANULATOR(23,10)|MIXED SLURRY(23,9)|AVERAGE PARTICLE DIAMETER(22,11)|ROLLING(22,10)|SPRAY HEAD(22,10)|BALL PROPORTION(22,2)|CAO CONTENT(22,2)|STACKING DENSITY(22,2)|THOUGHT(22,2)|BAKING FREE CERAMIC PARTICLE(21,10)|WATER PURIFICATION(21,2)|FE CONTENT(20,2)|FLY ASH(19,12)|AIRSPEED(19,2)|CARBON FIXING(18,44)|SOLID CONTENT(18,11)|ROTATING SPEED(18,3)|CARBON FIXING PRODUCT(18,1)|MASS FRACTION(18,1)|CARBON FIXATION(17,12)|DISPERSING AGENT(17,12)|CARBON DIOXIDE(17,4)|CEMENT(16,10)|SPRAYING(16,10)|SLURRY(16,9)|CALCIUM ION DISSOLUTION(16,3)|SLAG(16,2)|FLUE GAS INTRODUCTION(16,1)|ROLLING MATERIAL(14,10)|SODIUM HEXAMETAPHOSPHATE(13,2)|GRINDING LIQUID PHASE(13,1)|VALUE ADDED UTILIZATION(12,3)|AVERAGE PARTICLE SIZE(12,1)|AMMONIUM NITRATE(11,3)|POLYETHYLENE GLYCOL(11,2)|AMMONIUM SULFATE(10,3)|ARSENIC ADSORPTION(10,2)|AMMONIUM ACETATE(9,4)|AMMONIUM CHLORIDE(9,3)|SCREEN RESIDUE 3MCUMULATIVE(9,1)|FUNCTIONAL BAKING FREE CERAMSITE(8,5)|AUXILIARY ADMIXTURE(8,2)|SODIUM DODECYL BENZENE SULFONATE(8,2)|FRACTIONAL SCREEN RESIDUE CALCULATION(8,1)|STEEL SLAG MICROPOWDER(8,1)|SYNERGISTIC WET GRINDING(8,1)|ADDED VALUE UTILIZATION(7,2)|ADSORPTION EXPERIMENT(7,1)|DEFINITION FINENESS MODULUS(7,1)|MINERALIZATION CALCULATION(7,1)|CONTACT AREA(6,2)|ELEVATION ANGLE(6,2)|MAXIMUM PARTICLE SIZE(6,2)|CACO ANALYSIS(6,1)|CERAMSITE BASIC PERFORMANCE(6,1)|CERAMSITE PERFORMANCE(6,1)|FINENESS MODULUS MEASUREMENT(6,1)|RAW MATERIAL(5,16)|SIEVE(5,5)|POLYETHYLENE PLASTIC BOTTLE(5,2)|ADSORPTION REACTION(4,1)|CARBON FIXING ADSORPTION(4,1)|CARBONIZATION REACTION(4,1)|CONCENTRATIONWHEN(4,1)|CORROSION COUPLING(4,1)|CUMULATIVE PERCENT(4,1)| (CN116832605)|1. The method for functionally utilizing the flue gas catcher of the coal-fired power plant is characterized by comprising the following steps of:| 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; | 2) Uniformly mixing 20-50 parts by weight of steel slag micro powder and 1-5 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be 12.5% -33.3% to obtain a mixed slurry A; | 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, and introducing coal-fired flue gas to obtain a carbon-fixing functional admixture; | 4) Uniformly mixing 20-40 parts by weight of carbon fixation function admixture, 40-80 parts by weight of cement, 30-55 parts by weight of fly ash and 7-15 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; | 5) Starting a granulator, then slowly sprinkling water for 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting a spray head, slightly converging a streamline shape, and slowly spraying water by aiming at the edge part of the rolling material to prepare the carbon-fixing function baking-free ceramsite; | the maximum particle size of the perlite particles is not higher than 2.63mm, and the particle size range of the fly ash is 0.5-300 mu m; | The rotating speed of the circular pan granulator is 10-50 r/min, and the elevation angle of the circular pan granulator is 20-45 degrees; | The median particle diameter of the steel slag micro powder is 40-60 mu m, the CaO content of the steel slag micro powder is not lower than 30%, and the Fe 2O3 content of the steel slag micro powder is not lower than 15%; | The solid content represents the proportion of the mixture to water, and the ammonium salt is one of ammonium nitrate, ammonium chloride, ammonium acetate and ammonium sulfate; | the dispersing agent is one of sodium dodecyl benzene sulfonate, sodium hexametaphosphate and polyethylene glycol, the pH value of the carbon fixing functional admixture is 7-8, the median particle diameter is 2-5 mu m, and the content of Fe (OH) 3 is not less than 15%; | the sprinkling lasts for 0.5-2 s, each sprinkling interval is 5-10 s, one sprinkling lasts for 1-3 s, and each sprinkling interval is 7-15 s. |2. The method for functionally utilizing the flue gas catcher of the coal-fired power plant according to claim 1, wherein the concentration of CO 2 in the introduced coal-fired flue gas is not lower than 12% and the gas velocity is 5-12L/min.|3. The method for functionally utilizing the flue gas catcher of the coal-fired power plant according to claim 1, wherein the rotating speed of the stirring ball mill is 300-900 r/min, and the ball proportion of the stirring ball mill is m (0.5-0.8 mm): m (0.8-1.1 mm): m (1.1-1.4 mm) = (1-3): 1.|4. The method for functionally utilizing the flue gas catcher of the coal-fired power plant according to claim 1, wherein the fineness modulus of the ceramsite is 3.2-3.8, and the stacking density is 442.7kg/m < 3 > -581.1 kg/m < 3 >. (CN116832605)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of carbon dioxide sequestration and water purification, in particular to a method for functionally utilizing a flue gas collector of a coal-fired power plant.|BACKGROUND ART|[0002] The invention of Chinese patent CN108262016A, a method for removing carbon dioxide in gas by adsorption of steel slag, and CN103111186B, a method for strengthening mineralization of steel slag and fixing carbon dioxide, all have the problems of high carbon fixing cost, low carbon fixing efficiency, incapability of multi-scene application of carbon fixing products and the like.|[0003] At present, the domestic steel slag has lower additional value utilization, how to utilize the steel slag to seal and store CO 2 of the coal-fired power plant and realize the high additional value utilization of the steel slag, the permanent seal and the functional utilization of carbon-fixing products of CO 2 of the coal-fired power plant, and the aim of treating waste with waste and being environment-friendly is achieved, which is a problem to be solved by the current technicians in the field.|DISCLOSURE|Disclosure of Invention|[0004] (One) solving the technical problems|[0005] Aiming at the defects of the prior art, the invention provides a method for functionally utilizing the coal-fired power plant flue gas catcher, which has the advantages of high value-added utilization of steel slag and the like, and solves the problem of low value-added utilization of the existing steel slag.|[0006] (II) technical scheme|[0007] In order to achieve the purpose of high value-added utilization of the steel slag, the invention provides the following technical scheme:|[0008] A method for functionally utilizing a flue gas catcher of a coal-fired power plant comprises the following steps: |[0009] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0010] 2) Uniformly mixing 20-50 parts by weight of steel slag micro powder and 1-5 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be 12.5% -33.3% to obtain a mixed slurry A; |[0011] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, and introducing coal-fired flue gas to obtain a carbon-fixing functional admixture; |[0012] 4) Uniformly mixing 20-40 parts by weight of carbon fixation function admixture, 40-80 parts by weight of cement, 30-55 parts by weight of fly ash and 7-15 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0013] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0014] Preferably, the median particle size of the steel slag micro powder is 40-60 mu m, the CaO content of the steel slag micro powder is not less than 30%, and the Fe 2O3 content of the steel slag micro powder is not less than 15%.|[0015] Preferably, the concentration of CO 2 in the introduced coal-fired flue gas is not lower than 12%, and the gas velocity is 5L/min-12L/min.|[0016] Preferably, the solid content represents the ratio of the mixture to water, and the ammonium salt is one of ammonium nitrate, ammonium chloride, ammonium acetate and ammonium sulfate.|[0017] Preferably, the rotation speed of the stirred ball mill is 300-900 r/min, and the ball proportion of the stirred ball mill is m (0.5-0.8 mm): m (0.8-1.1 mm): m (1.1-1.4 mm) = (1-3): 1.|[0018] Preferably, the dispersing agent is one of sodium dodecyl benzene sulfonate, sodium hexametaphosphate and polyethylene glycol, the pH value of the carbon-fixing functional admixture is 7-8, the median particle diameter reaches 2-5 mu m, and the content of Fe (OH) 3 is not less than 15%.|[0019] Preferably, the maximum particle size of the perlite particles is not higher than 2.63mm, and the particle size range of the fly ash is 0.5-300 mu m.|[0020] Preferably, the rotating speed of the circular pan granulator is 10-50 r/min, and the elevation angle of the circular pan granulator is 20-45 degrees.|[0021] Preferably, the sprinkling lasts about 0.5-2 s, each sprinkling interval is 5-10 s, each sprinkling interval lasts 1-3 s, each sprinkling interval is 7-15 s.|[0022] Preferably, the fineness modulus of the ceramsite is 3.2-3.8, and the stacking density is 442.7kg/m < 3 > -581.1 kg/m < 3 >.|[0023] The method has the following mechanism:|[0024] The invention provides a method for capturing flue gas of a coal-fired power plant and functionally utilizing captured products thereof. The carbon-fixing functional admixture is prepared by taking steel slag as a raw material, grinding in cooperation with ammonium salt, introducing coal-fired flue gas in the grinding process, and reacting until the pH value is 7-8, thereby preparing the carbon-fixing functional admixture with the median particle diameter of 2-5 mu m. The solid waste steel slag has high alkalinity and Ca element contained therein, has a certain carbon fixation potential, can react with CO2 in coal-fired flue gas to generate stable carbonate products, and the main reaction equation is as follows: |[0025] ;|[0026] The mineral components in the steel slag mainly comprise Ca2SiO3, ca3SiO5, ca2Fe2O5 and RO phases. Therefore, the calcium element in the steel slag is difficult to dissolve in the water medium under mild environmental conditions, so that the mineralization efficiency is low. The invention utilizes the physical mechanical force-chemical corrosion coupling, namely a liquid phase grinding process, fully breaks steel slag particles, promotes the dissolution of steel slag Ca 2+ ions, namely promotes the reaction a and b to be carried out, and simultaneously, the reaction a and b and the reaction b are cooperated with ammonium salt to be ground together, and the dissolution of CO 2 in water is increased due to the influence of NH 4+, namely the reaction c and d are promoted to be carried out. The reaction f is promoted by the two, so that CO 2 is efficiently stored, and the steel slag has higher carbon fixing efficiency. |[0027] Further, by controlling the solid content ratio to be 12.5% -33.3%, the fluidity of the material is improved, the grinding efficiency is further improved, the grinding time is controlled to be not lower than 30min, the ventilation speed is controlled to be not lower than 2L/min, the raw materials can be ensured to be ground to be 2-5 mu m, the dissolution of calcium ions is promoted, the ammonium salt is added in an auxiliary mode to assist in wet grinding, and the dissolution of carbon dioxide is accelerated, so that the carbon fixing efficiency is higher. Preferably, the ammonium salt is ammonium nitrate, ammonium chloride, ammonium acetate and ammonium sulfate, more preferably ammonium acetate.|[0028] Further, iron oxide in the steel slag and CO 2 are subjected to carbonization reaction to generate FeCO 3/Fe2(CO3)3, and then FeCO 3/Fe2(CO3)3 is subjected to hydrolysis reaction to generate Fe (OH) 3, so that the carbon-fixing functional admixture contains Fe (OH) 3, Fe(OH)3 and has good adsorption effect on arsenic, the carbon-fixing functional admixture is doped into ceramsite instead of part of gelled materials, perlite particles are nucleation sites, the carbon-fixing functional baking-free ceramsite is prepared, the steel slag is effectively utilized on the premise of ensuring the basic performance of the ceramsite, carbon dioxide discharged by a coal-fired power plant can be effectively trapped, and the ceramsite has good application prospect in arsenic adsorption in water treatment. The invention provides a new thought and a new method for the high added value utilization of the steel slag, and the solid waste is used for purifying the water body, so that waste is turned into wealth.|[0029] (III) beneficial effects|[0030] Compared with the prior art, the invention provides a method for functionally utilizing the flue gas catcher of the coal-fired power plant, which has the following beneficial effects:|[0031] 1. According to the method for functionally utilizing the flue gas catcher of the coal-fired power plant, the steel slag is taken as a main raw material, the liquid-phase grinding is cooperated with the ammonium salt, and the coal-fired flue gas is introduced, so that on one hand, the liquid-phase grinding sufficiently breaks up steel slag particles, the contact area between CO 2 in the coal-fired flue gas and the steel slag is increased while the dissolution of calcium ions is promoted, on the other hand, the ammonium salt grinding is cooperated, the dissolution of CO 2 is promoted, and on the other hand, the carbon fixation efficiency of the steel slag is improved. |[0032] 2. According to the method for functionally utilizing the flue gas catcher of the coal-fired power plant, fe (OH) 3 is contained in the steel slag carbon fixation product to prepare the carbon fixation function admixture, the carbon fixation function admixture is used for preparing carbon fixation function baking-free ceramsite, and the ceramsite has a good adsorption effect on arsenic in a water body, so that the utilization added value of the steel slag is improved.|DRAWINGS DESCRIPTION|[0033] Fig. 1 is a test chart of an embodiment of a method for functionally utilizing a flue gas catcher of a coal-fired power plant.|INVENTION MODE|Detailed Description|[0034] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0035] Embodiment one:|[0036] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0037] 2) Uniformly mixing 25 parts by weight of steel slag micro powder and 1 part by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0038] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0039] 4) Uniformly mixing the carbon-fixing functional admixture, 40 parts by weight of cement, 30 parts by weight of fly ash and 7 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0040] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0041] Embodiment two:|[0042] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0043] 2) Uniformly mixing 30 parts by weight of steel slag micro powder and 2 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0044] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0045] 4) Uniformly mixing carbon-fixing functional admixture, 45 parts by weight of cement, 35 parts by weight of fly ash and 9 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0046] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0047] Embodiment III:|[0048] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0049] 2) Uniformly mixing 35 parts by weight of steel slag micro powder and 4 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0050] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0051] 4) Uniformly mixing the carbon-fixing functional admixture, 55 parts by weight of cement, 40 parts by weight of fly ash and 10 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0052] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0053] Embodiment four:|[0054] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0055] 2) Uniformly mixing 40 parts by weight of steel slag micro powder and 3 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0056] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0057] 4) Uniformly mixing the carbon-fixing functional admixture, 65 parts by weight of cement, 43 parts by weight of fly ash and 12 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0058] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0059] Fifth embodiment:|[0060] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0061] 2) Uniformly mixing 45 parts by weight of steel slag micro powder and 4 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0062] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0063] 4) Uniformly mixing the carbon-fixing functional admixture, 70 parts by weight of cement, 50 parts by weight of fly ash and 14 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0064] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0065] Example six:|[0066] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0067] 2) Uniformly mixing 50 parts by weight of steel slag micro powder and 5 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0068] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0069] 4) Uniformly mixing the carbon-fixing functional admixture, 80 parts by weight of cement, 55 parts by weight of fly ash and 15 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0070] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0071] Comparative example one:|[0072] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0073] 2) Adding water into 25 parts by weight of steel slag micro powder, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain mixed slurry A; |[0074] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0075] 4) Uniformly mixing the carbon-fixing functional admixture, 40 parts by weight of cement, 30 parts by weight of fly ash and 7 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0076] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0077] Comparative example two:|[0078] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0079] 2) Uniformly mixing 25 parts by weight of steel slag micro powder and 1 part by weight of ammonium salt to obtain a mixture A; |[0080] 3) Placing the mixture A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting at a gas speed of 5L/min until the PH=7-8, and obtaining a carbon-fixing functional admixture; |[0081] 4) Uniformly mixing the carbon-fixing functional admixture, 40 parts by weight of cement, 30 parts by weight of fly ash and 7 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0082] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0083] Experimental example:|[0084] The arsenic adsorption rate is measured by preparing an arsenic-containing water sample with the concentration of 1mol/L by using As 2O5, diluting the water sample step by using ultrapure water during an adsorption experiment, firstly accurately weighing the carbon-fixing function baking-free ceramsite in a polyethylene plastic bottle, then adding an As (V) containing solution with the pH value adjusted in advance, the arsenic concentration of 0.000001-1 mol/L and the volume of 50mL into the polyethylene plastic bottle filled with the carbon-fixing function baking-free ceramsite, covering a bottle cap, shaking the bottle cap uniformly, standing for 50d (shaking for several times by hands each time for about 2 min) at room temperature (23+/-1) DEGC), and measuring the adsorption rate of the carbon-fixing function baking-free ceramsite to arsenic by adopting a graphite furnace atomic absorption spectrometry after the adsorption reaction of 50 d. |[0085] And (3) measuring carbon fixation efficiency, namely measuring the loss weight of CaCO 3 in raw materials and products by TG analysis, wherein the definition of the mineralization efficiency and mineralization efficiency is defined as the capacity of fixing CO 2 by alkaline solid waste and is equal to the ratio of the mass of the fixed CO 2 to the mass of the alkaline solid waste.|[0086] ;|[0087] M1 represents the mass of CO 2 immobilized after mineralization;|[0088] m2 represents the mass of the alkaline solid waste. |[0089] The fineness modulus is measured, namely, the fineness modulus is expressed by adopting a fractional screen residue calculation method in the current national standard 'sand for construction' GB/T14684, and the fineness modulus is defined to be 3.2-3.8 mm, and the closer to 3.5mm, the better the ceramsite performance.|[0090] M=(A2+A3+A4+A5+A6-5A1)/(100-A1);|[0091] M-fineness modulus;|[0092] a 1 -cumulative percent screen residue for a 4.75mm sieve; |[0093] A 2 -cumulative percent screen residue for a 2.36mm sieve; |[0094] A 3 -cumulative percentage of screen residue for a 1.18mm sieve; |[0095] a 4 -cumulative percentage of screen residue for a 0.6mm sieve; |[0096] A 5 -cumulative percentage of screen residue for a 0.3mm sieve; |[0097] a 6 -cumulative percent screen residue for a 0.15mm sieve. |[0098] As shown in fig. 1, as can be seen from fig. 1, the comparative example 1 is not added with ammonium salt to cooperate with wet milling, the comparative example 2 is not subjected to wet milling treatment, and compared with the comparative example 1, the fineness modulus of the ceramsite of the comparative example 1 and the comparative example 2, the As adsorption efficiency and the carbon fixation efficiency are far lower than those of the example 1, and the effect is not ideal;|[0099] Compared with comparative examples 1-2, examples 1-6 can significantly seal CO 2, carbon-fixing functional additives prepared from steel slag after carbon fixing are used As auxiliary additives, the adsorption efficiency of carbon-fixing functional baking-free ceramsite prepared by the auxiliary additives on As is 90% -97%, the carbon-fixing efficiency is 31.4% -42.1%, and the fineness modulus of the ceramsite is 3.2-3.8 mm. Of these, example 3 had the best overall performance. |[0100] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. (CN116832605)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of carbon dioxide sequestration and water purification, in particular to a method for functionally utilizing a flue gas collector of a coal-fired power plant.|BACKGROUND ART|[0002] The invention of Chinese patent CN108262016A, a method for removing carbon dioxide in gas by adsorption of steel slag, and CN103111186B, a method for strengthening mineralization of steel slag and fixing carbon dioxide, all have the problems of high carbon fixing cost, low carbon fixing efficiency, incapability of multi-scene application of carbon fixing products and the like.|[0003] At present, the domestic steel slag has lower additional value utilization, how to utilize the steel slag to seal and store CO 2 of the coal-fired power plant and realize the high additional value utilization of the steel slag, the permanent seal and the functional utilization of carbon-fixing products of CO 2 of the coal-fired power plant, and the aim of treating waste with waste and being environment-friendly is achieved, which is a problem to be solved by the current technicians in the field.|DISCLOSURE|Disclosure of Invention|[0004] (One) solving the technical problems|[0005] Aiming at the defects of the prior art, the invention provides a method for functionally utilizing the coal-fired power plant flue gas catcher, which has the advantages of high value-added utilization of steel slag and the like, and solves the problem of low value-added utilization of the existing steel slag.|[0006] (II) technical scheme|[0007] In order to achieve the purpose of high value-added utilization of the steel slag, the invention provides the following technical scheme:|[0008] A method for functionally utilizing a flue gas catcher of a coal-fired power plant comprises the following steps: |[0009] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0010] 2) Uniformly mixing 20-50 parts by weight of steel slag micro powder and 1-5 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be 12.5% -33.3% to obtain a mixed slurry A; |[0011] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, and introducing coal-fired flue gas to obtain a carbon-fixing functional admixture; |[0012] 4) Uniformly mixing 20-40 parts by weight of carbon fixation function admixture, 40-80 parts by weight of cement, 30-55 parts by weight of fly ash and 7-15 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0013] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0014] Preferably, the median particle size of the steel slag micro powder is 40-60 mu m, the CaO content of the steel slag micro powder is not less than 30%, and the Fe 2O3 content of the steel slag micro powder is not less than 15%.|[0015] Preferably, the concentration of CO 2 in the introduced coal-fired flue gas is not lower than 12%, and the gas velocity is 5L/min-12L/min.|[0016] Preferably, the solid content represents the ratio of the mixture to water, and the ammonium salt is one of ammonium nitrate, ammonium chloride, ammonium acetate and ammonium sulfate.|[0017] Preferably, the rotation speed of the stirred ball mill is 300-900 r/min, and the ball proportion of the stirred ball mill is m (0.5-0.8 mm): m (0.8-1.1 mm): m (1.1-1.4 mm) = (1-3): 1.|[0018] Preferably, the dispersing agent is one of sodium dodecyl benzene sulfonate, sodium hexametaphosphate and polyethylene glycol, the pH value of the carbon-fixing functional admixture is 7-8, the median particle diameter reaches 2-5 mu m, and the content of Fe (OH) 3 is not less than 15%.|[0019] Preferably, the maximum particle size of the perlite particles is not higher than 2.63mm, and the particle size range of the fly ash is 0.5-300 mu m.|[0020] Preferably, the rotating speed of the circular pan granulator is 10-50 r/min, and the elevation angle of the circular pan granulator is 20-45 degrees.|[0021] Preferably, the sprinkling lasts about 0.5-2 s, each sprinkling interval is 5-10 s, each sprinkling interval lasts 1-3 s, each sprinkling interval is 7-15 s.|[0022] Preferably, the fineness modulus of the ceramsite is 3.2-3.8, and the stacking density is 442.7kg/m < 3 > -581.1 kg/m < 3 >.|[0023] The method has the following mechanism:|[0024] The invention provides a method for capturing flue gas of a coal-fired power plant and functionally utilizing captured products thereof. The carbon-fixing functional admixture is prepared by taking steel slag as a raw material, grinding in cooperation with ammonium salt, introducing coal-fired flue gas in the grinding process, and reacting until the pH value is 7-8, thereby preparing the carbon-fixing functional admixture with the median particle diameter of 2-5 mu m. The solid waste steel slag has high alkalinity and Ca element contained therein, has a certain carbon fixation potential, can react with CO2 in coal-fired flue gas to generate stable carbonate products, and the main reaction equation is as follows: |[0025] ;|[0026] The mineral components in the steel slag mainly comprise Ca2SiO3, ca3SiO5, ca2Fe2O5 and RO phases. Therefore, the calcium element in the steel slag is difficult to dissolve in the water medium under mild environmental conditions, so that the mineralization efficiency is low. The invention utilizes the physical mechanical force-chemical corrosion coupling, namely a liquid phase grinding process, fully breaks steel slag particles, promotes the dissolution of steel slag Ca 2+ ions, namely promotes the reaction a and b to be carried out, and simultaneously, the reaction a and b and the reaction b are cooperated with ammonium salt to be ground together, and the dissolution of CO 2 in water is increased due to the influence of NH 4+, namely the reaction c and d are promoted to be carried out. The reaction f is promoted by the two, so that CO 2 is efficiently stored, and the steel slag has higher carbon fixing efficiency. |[0027] Further, by controlling the solid content ratio to be 12.5% -33.3%, the fluidity of the material is improved, the grinding efficiency is further improved, the grinding time is controlled to be not lower than 30min, the ventilation speed is controlled to be not lower than 2L/min, the raw materials can be ensured to be ground to be 2-5 mu m, the dissolution of calcium ions is promoted, the ammonium salt is added in an auxiliary mode to assist in wet grinding, and the dissolution of carbon dioxide is accelerated, so that the carbon fixing efficiency is higher. Preferably, the ammonium salt is ammonium nitrate, ammonium chloride, ammonium acetate and ammonium sulfate, more preferably ammonium acetate.|[0028] Further, iron oxide in the steel slag and CO 2 are subjected to carbonization reaction to generate FeCO 3/Fe2(CO3)3, and then FeCO 3/Fe2(CO3)3 is subjected to hydrolysis reaction to generate Fe (OH) 3, so that the carbon-fixing functional admixture contains Fe (OH) 3, Fe(OH)3 and has good adsorption effect on arsenic, the carbon-fixing functional admixture is doped into ceramsite instead of part of gelled materials, perlite particles are nucleation sites, the carbon-fixing functional baking-free ceramsite is prepared, the steel slag is effectively utilized on the premise of ensuring the basic performance of the ceramsite, carbon dioxide discharged by a coal-fired power plant can be effectively trapped, and the ceramsite has good application prospect in arsenic adsorption in water treatment. The invention provides a new thought and a new method for the high added value utilization of the steel slag, and the solid waste is used for purifying the water body, so that waste is turned into wealth.|[0029] (III) beneficial effects|[0030] Compared with the prior art, the invention provides a method for functionally utilizing the flue gas catcher of the coal-fired power plant, which has the following beneficial effects:|[0031] 1. According to the method for functionally utilizing the flue gas catcher of the coal-fired power plant, the steel slag is taken as a main raw material, the liquid-phase grinding is cooperated with the ammonium salt, and the coal-fired flue gas is introduced, so that on one hand, the liquid-phase grinding sufficiently breaks up steel slag particles, the contact area between CO 2 in the coal-fired flue gas and the steel slag is increased while the dissolution of calcium ions is promoted, on the other hand, the ammonium salt grinding is cooperated, the dissolution of CO 2 is promoted, and on the other hand, the carbon fixation efficiency of the steel slag is improved. |[0032] 2. According to the method for functionally utilizing the flue gas catcher of the coal-fired power plant, fe (OH) 3 is contained in the steel slag carbon fixation product to prepare the carbon fixation function admixture, the carbon fixation function admixture is used for preparing carbon fixation function baking-free ceramsite, and the ceramsite has a good adsorption effect on arsenic in a water body, so that the utilization added value of the steel slag is improved.|DRAWINGS DESCRIPTION|[0033] Fig. 1 is a test chart of an embodiment of a method for functionally utilizing a flue gas catcher of a coal-fired power plant.|INVENTION MODE|Detailed Description|[0034] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0035] Embodiment one:|[0036] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0037] 2) Uniformly mixing 25 parts by weight of steel slag micro powder and 1 part by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0038] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0039] 4) Uniformly mixing the carbon-fixing functional admixture, 40 parts by weight of cement, 30 parts by weight of fly ash and 7 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0040] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0041] Embodiment two:|[0042] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0043] 2) Uniformly mixing 30 parts by weight of steel slag micro powder and 2 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0044] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0045] 4) Uniformly mixing carbon-fixing functional admixture, 45 parts by weight of cement, 35 parts by weight of fly ash and 9 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0046] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0047] Embodiment III:|[0048] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0049] 2) Uniformly mixing 35 parts by weight of steel slag micro powder and 4 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0050] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0051] 4) Uniformly mixing the carbon-fixing functional admixture, 55 parts by weight of cement, 40 parts by weight of fly ash and 10 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0052] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0053] Embodiment four:|[0054] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0055] 2) Uniformly mixing 40 parts by weight of steel slag micro powder and 3 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0056] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0057] 4) Uniformly mixing the carbon-fixing functional admixture, 65 parts by weight of cement, 43 parts by weight of fly ash and 12 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0058] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0059] Fifth embodiment:|[0060] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0061] 2) Uniformly mixing 45 parts by weight of steel slag micro powder and 4 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0062] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0063] 4) Uniformly mixing the carbon-fixing functional admixture, 70 parts by weight of cement, 50 parts by weight of fly ash and 14 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0064] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0065] Example six:|[0066] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0067] 2) Uniformly mixing 50 parts by weight of steel slag micro powder and 5 parts by weight of ammonium salt to obtain a mixture, adding water, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain a mixed slurry A; |[0068] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0069] 4) Uniformly mixing the carbon-fixing functional admixture, 80 parts by weight of cement, 55 parts by weight of fly ash and 15 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0070] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0071] Comparative example one:|[0072] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0073] 2) Adding water into 25 parts by weight of steel slag micro powder, and adjusting the solid content to be between 12.5 and 33.3 percent to obtain mixed slurry A; |[0074] 3) Placing the slurry A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting until the PH=7-8 and the median particle diameter reaches 5 mu m, and obtaining a carbon-fixing functional admixture; |[0075] 4) Uniformly mixing the carbon-fixing functional admixture, 40 parts by weight of cement, 30 parts by weight of fly ash and 7 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0076] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0077] Comparative example two:|[0078] 1) Taking steel slag as a raw material, primarily grinding the massive steel slag to obtain steel slag coarse powder, and grinding the steel slag coarse powder again to obtain steel slag micro powder; |[0079] 2) Uniformly mixing 25 parts by weight of steel slag micro powder and 1 part by weight of ammonium salt to obtain a mixture A; |[0080] 3) Placing the mixture A into a stirred ball mill, grinding for 10min, adding a dispersing agent, continuously grinding, introducing coal-fired flue gas, reacting at a gas speed of 5L/min until the PH=7-8, and obtaining a carbon-fixing functional admixture; |[0081] 4) Uniformly mixing the carbon-fixing functional admixture, 40 parts by weight of cement, 30 parts by weight of fly ash and 7 parts by weight of perlite particles, and pouring the mixture into a circular pan granulator; |[0082] 5) Starting the granulator, then slowly sprinkling water for about 1min, observing that spherical particles are formed in the central part of the rolling material, slightly adjusting the spray head, slightly converging the water to be streamline, and slowly spraying water to the edge part of the rolling material by the spray head to prepare the carbon-fixing function baking-free ceramic particles. |[0083] Experimental example:|[0084] The arsenic adsorption rate is measured by preparing an arsenic-containing water sample with the concentration of 1mol/L by using As 2O5, diluting the water sample step by using ultrapure water during an adsorption experiment, firstly accurately weighing the carbon-fixing function baking-free ceramsite in a polyethylene plastic bottle, then adding an As (V) containing solution with the pH value adjusted in advance, the arsenic concentration of 0.000001-1 mol/L and the volume of 50mL into the polyethylene plastic bottle filled with the carbon-fixing function baking-free ceramsite, covering a bottle cap, shaking the bottle cap uniformly, standing for 50d (shaking for several times by hands each time for about 2 min) at room temperature (23+/-1) DEGC), and measuring the adsorption rate of the carbon-fixing function baking-free ceramsite to arsenic by adopting a graphite furnace atomic absorption spectrometry after the adsorption reaction of 50 d. |[0085] And (3) measuring carbon fixation efficiency, namely measuring the loss weight of CaCO 3 in raw materials and products by TG analysis, wherein the definition of the mineralization efficiency and mineralization efficiency is defined as the capacity of fixing CO 2 by alkaline solid waste and is equal to the ratio of the mass of the fixed CO 2 to the mass of the alkaline solid waste.|[0086] ;|[0087] M1 represents the mass of CO 2 immobilized after mineralization;|[0088] m2 represents the mass of the alkaline solid waste. |[0089] The fineness modulus is measured, namely, the fineness modulus is expressed by adopting a fractional screen residue calculation method in the current national standard 'sand for construction' GB/T14684, and the fineness modulus is defined to be 3.2-3.8 mm, and the closer to 3.5mm, the better the ceramsite performance.|[0090] M=(A2+A3+A4+A5+A6-5A1)/(100-A1);|[0091] M-fineness modulus;|[0092] a 1 -cumulative percent screen residue for a 4.75mm sieve; |[0093] A 2 -cumulative percent screen residue for a 2.36mm sieve; |[0094] A 3 -cumulative percentage of screen residue for a 1.18mm sieve; |[0095] a 4 -cumulative percentage of screen residue for a 0.6mm sieve; |[0096] A 5 -cumulative percentage of screen residue for a 0.3mm sieve; |[0097] a 6 -cumulative percent screen residue for a 0.15mm sieve. |[0098] As shown in fig. 1, as can be seen from fig. 1, the comparative example 1 is not added with ammonium salt to cooperate with wet milling, the comparative example 2 is not subjected to wet milling treatment, and compared with the comparative example 1, the fineness modulus of the ceramsite of the comparative example 1 and the comparative example 2, the As adsorption efficiency and the carbon fixation efficiency are far lower than those of the example 1, and the effect is not ideal;|[0099] Compared with comparative examples 1-2, examples 1-6 can significantly seal CO 2, carbon-fixing functional additives prepared from steel slag after carbon fixing are used As auxiliary additives, the adsorption efficiency of carbon-fixing functional baking-free ceramsite prepared by the auxiliary additives on As is 90% -97%, the carbon-fixing efficiency is 31.4% -42.1%, and the fineness modulus of the ceramsite is 3.2-3.8 mm. Of these, example 3 had the best overall performance. |[0100] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. Family Number|(106744235)|106744235|Abstract|(CN116832605B B)|The invention relates to the technical field of carbon dioxide sequestration and water purification , in particular to a method for functionalized utilization of flue gas traps of a coal - fired power plant , and discloses the method for functionalized utilization of the flue gas traps of the coal - fired power plant , which comprises the following steps : taking steel slag as a raw material , performing primary grinding on blocky steel slag to obtain steel slag coarse powder , performing secondary grinding , and performing secondary grinding to obtain the flue gas traps of the coal - fired power plant . Steel slag micro powder is obtained ; 20-50 parts by weight of steel slag micro powder and 1-5 parts by weight of ammonium salt are evenly mixed , a mixture is obtained , and water is added . According to the method for functionalized utilization of the flue gas traps of the coal - fired power plant , steel slag is used as a main raw material and cooperates with ammonium salt liquid - phase grinding , coal - fired flue gas is introduced , on one hand , steel slag particles are fully crushed through liquid - phase grinding , the contact area of CO2 in the coal - fired flue gas and the steel slag is increased while calcium ion dissolution is promoted , on the other hand , CO2 dissolution can be promoted through cooperation with ammonium salt grinding , and the CO2 content in the coal - fired flue gas is increased . Meanwhile , the steel slag carbon sequestration efficiency is improved . |CPC codes|(CN116832605B B)|B01D - 053/62 |B01D - 053/80 |B01D - 2257/504 |B01D - 2258/0283 |B01J - 020/12 |IPC codes|(CN116832605B B)|B01D - 053/62 |B01D - 053/80 |B01J - 020/12 | Chemical engineering|Environmental technology B01D-053/02|B01D-053/62|B01D-053/80|B01D-053/81|B01D-2251/404|B01D-2257/504|B01D-2257/60|B01D-2257/602|B01D-2258/0283|B01J-020/02|B01J-020/02/48|B01J-020/04/1|B01J-020/04/3|B01J-020/06|B01J-020/08|B01J-020/12|B01J-020/30/21|B01J-020/30/28|B01J-020/30/78|B01J-2220/42|C02F-001/28/1|C02F-2101/103|C02F-2101/105|Y02C-010/04|Y02P-020/152 B01D-053/02|B01D-053/62|B01D-053/80|B01D-053/81|B01D-2251/404|B01D-2257/504|B01D-2257/60|B01D-2257/602|B01D-2258/0283|B01J-020/02|B01J-020/02/48|B01J-020/04/1|B01J-020/04/3|B01J-020/06|B01J-020/08|B01J-020/12|B01J-020/30/21|B01J-020/30/28|B01J-020/30/78|B01J-2220/42|C02F-001/28/1|C02F-2101/103|C02F-2101/105|Y02C-010/04|Y02P-020/152 B01D-053/62|B01D-053/80|B01J-020/12|C02F-001/28|C02F-101/10 B01D-053/62|B01D-053/80|B01J-020/12|C02F-001/28|C02F-101/10 CN114832770|CN114804685|JP2017214262|CN102794093|KR20130002129|CN102114383|CN101920983|CN115069362|CN110950607|CN102992372 CN114832770 101160281 WHO=Examiner SELF=N CAT=A|CN114804685 101081449 WHO=Examiner SELF=N CAT=A|JP2017214262 77993560 WHO=Examiner SELF=N CAT=A|CN102794093 7992542 WHO=Examiner SELF=N CAT=A|KR20130002129 35392161 WHO=Examiner SELF=N CAT=A|CN102114383 7351345 WHO=Examiner SELF=N CAT=A|CN101920983 7168018 WHO=Examiner SELF=N CAT=A|CN115069362 101844296 WHO=Examiner SELF=Y|CN110950607 88106357 WHO=Examiner SELF=N|CN102992372 14283060 WHO=Examiner SELF=N CN101920983; CN102114383; KR20130002129; JP2017214262; CN114832770; CN102794093; CN114804685; CN115069362; CN102992372; CN110950607 GRANTED (CN116832605)|GRANTED ALIVE (CN116832605)|ALIVE (CN116832605)|LEGAL DETAILS FOR CN116832605|Actual or expected expiration date=2043-03-06|Legal state=ALIVE|Status=GRANTED|Event publication date=2023-03-06|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202310205820|Application date=2023-03-06|Standardized application number=2023CN-0205820|Event publication date=2023-10-03|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN116832605|Publication stage code=A|Publication date=2023-10-03|Standardized publication number=CN116832605|Event publication date=2023-10-03|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-10-24|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2026-04-14|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN116832605|Publication stage code=B|Publication date=2026-04-14|Standardized publication number=CN116832605B|Event publication date=2026-04-14|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN116832605)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSzucEsAbeViRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000081521604&ekey=2180&xpn=CN116832605B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=jU1F0QbHFtRU7ZKU3kEIjrmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN116832605)|CN|(CN116832605)|CN (CN116832605)|NAME=HUBEI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN|(CN116832605)|NAME=HUBEI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN116832605)|NAME=QIAN CHUNHU;WUHAN SINOPOWER PATENT AGENCY , REG=42237|(CN116832605)|NAME=QIAN CHUNHU;WUHAN SINOPOWER PATENT AGENCY , REG=42237 (CN116832605)|CN| (CN116832605)|NAME=HE XINGYANG, COUNTRY=CN |NAME=XIAO HUCHENG|NAME=YANG JIN|NAME=SU YING|NAME=DAI FEI|NAME=WANG YINGBIN|NAME=LIU SENYE|NAME=ZHANG JUNHUN|NAME=WANG ZHIRUI|(CN116832605)|NAME=HE XINGYANG|NAME=XIAO HUCHENG|NAME=YANG JIN|NAME=SU YING|NAME=DAI FEI|NAME=WANG YINGBIN|NAME=LIU SENYE|NAME=ZHANG JUNHUN|NAME=WANG ZHIRUI 0 1 Titre: (CN116832605)|Method for functionally utilizing smoke catcher of coal-fired power plant Résumé: (CN116832605)|The invention relates to the technical field of carbon dioxide sequestration and water purification, in particular to a method for functionalized utilization of flue gas traps of a coal-fired power plant, and discloses the method for functionalized utilization of the flue gas traps of the coal-fired power plant, which comprises the following steps: taking steel slag as a raw material, performing primary grinding on blocky steel slag to obtain steel slag coarse powder, performing secondary grinding, and performing secondary grinding to obtain the flue gas traps of the coal-fired power plant. Steel slag micro powder is obtained; 20-50 parts by weight of steel slag micro powder and 1-5 parts by weight of ammonium salt are evenly mixed, a mixture is obtained, and water is added. According to the method for functionalized utilization of the flue gas traps of the coal-fired power plant, steel slag is used as a main raw material and cooperates with ammonium salt liquid-phase grinding, coal-fired flue gas is introduced, on one hand, steel slag particles are fully crushed through liquid-phase grinding, the contact area of CO2 in the coal-fired flue gas and the steel slag is increased while calcium ion dissolution is promoted, on the other hand, CO2 dissolution can be promoted through cooperation with ammonium salt grinding, and the CO2 content in the coal-fired flue gas is increased. Meanwhile, the steel slag carbon sequestration efficiency is improved. 101 Abstract gpt-4o-mini no The article focuses on the functionalized utilization of flue gas traps from coal-fired power plants, specifically involving steel slag and ammonium salts, rather than directly addressing accelerated weathering or mineral carbonation for CO2 sequestration.
104 CN201510198643 CN201510198643 CN104865306 70706682 CN104865306 A 2015-08-26 [CN104865306] 2015-04-23 2015-04-23 2015-08-26 (CN104865306)|2018-03-16 (CN104865306)|Detection method of adsorbable organic chlorides in solid sample (CN104865306)|The invention discloses a detection method of adsorbable organic chlorides in a solid sample, belongs to the measurement technology, and can solve the problem of detection of content of adsorbable organic chloride in the solid sample. According to the method, the solid sample is treated by crushing, adsorbing with activated carbon, removal of inorganic chlorine with nitrate and nitric acid, filtering, burning at 1000 DEG C, micro coulomb titration and other steps, and the content of AOX (absorbable organic halogen) content in the solid sample can be calculated. According to the method, the influence of the inorganic chloride can be fully eliminated, and the content of the AOX (absorbable organic halogen) content in the solid sample can be accurately analyzed. CHINA MATIONAL PULP & PAPER RESEARCH INSTITUTE (CN104865306)|CHINA MATIONAL PULP & PAPER RESEARCH INSTITUTE ZHANG SHENGYOU|SU ZHENHUA|CAO YINGGE|ZHANG YU|FENG WENYING|LIANG FANGYUAN (CN104865306)|ZHANG SHENGYOU|SU ZHENHUA|CAO YINGGE|ZHANG YU|FENG WENYING|LIANG FANGYUAN (CN104865306)|The invention has the following advantages:|Therefore, in view of the hazard of AOX, there is a need to establish a unified detection method for AOX content in solid sample to adapt to the ever-increasing regulations and the ever-increasing green concept.|The AOX pollution of the paper industry is mainly derived from chlorine bleaching wastewater, and researches show that during the chlorine bleaching process of paper pulp, more than 500 organic chlorides such as trichloromethane, chlorinated phenols, chlorinated fatty acids and the like can be generated, the organic chlorides can cause diseases or death to biological accumulation when discharged into natural water, and can directly act on mammals and human beings through drinking water, and the harm is very large.| (CN104865306)|1. A detection method for adsorbable organic chloride in a solid sample is characterized by comprising the following steps: the method comprises the following steps:a. crushing a solid sample into powder of 60-100 meshes by using a crusher or scissors and other tools, and weighing 10-50 mg of powder into a conical flask with a ground stopper;b. 100ml of ultrapure water was added to the flask, and 5ml of Na was added2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;c. adding 50mg of activated carbon into the conical flask, plugging the bottle stopper tightly, placing the conical flask on an oscillator support plate, and oscillating and adsorbing for more than 6 hours;d. filtering the liquid in the conical flask by using a quartz filter bowl, washing the conical flask and the filter by 25mL of sodium nitrate washing liquid in a grading way, and finally washing by using a small amount of water;e. putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;f. and (3) absorbing hydrogen chloride generated by combustion by adopting electrolyte, and measuring the chlorine content in the electrolyte by using a micro coulometer to obtain the AOX content in the solid sample.| (CN104865306)|The invention aims to provide a method for detecting adsorbable organic chloride in a solid sample, which is simple, convenient, accurate, reliable and low in cost.|The invention discloses a method for detecting adsorbable organic chloride in a solid sample, belongs to the measurement technology, and can solve the problem of detecting the content of adsorbable organic chloride in the solid sample.| (CN104865306)|SOLID SAMPLE(100,17)|ADSORBABLE ORGANIC CHLORIDE DETECTION(100,5)|ADSORBABLE ORGANIC CHLORIDE(100,2)|CHLORINE BLEACH(100,1)|AOX HAZARD(72,1)|AOX POLLUTION(71,1)|AOX CONTENT(62,13)|MICRO COULOMETER(61,2)|CHLORINATED PHENOL(58,1)|COMBUSTION FURNACE(54,6)|UNIFIED DETECTION(53,1)|MICRO COULOMETRIC TITRATION(52,1)|SILICA BOAT(50,10)|SILICA FILTER BOWL(49,2)|INORGANIC CHLORINE INFLUENCE(47,1)|CONICAL FLASK(44,19)|GREEN CONCEPT(41,1)|TRICHLOROMETHANE(39,1)|FILTER BOWL(37,2)|FILTERED SILICA FILTER CUP(35,5)|INORGANIC CHLORINE REMOVAL(35,1)|ULTRAPURE WATER CONDUCTIVITY RESISTIVITY(35,1)|ELECTROLYTE(34,11)|SILICA FILTER CUP(34,5)|GROUND STOPPER(32,5)|GRADING(32,2)|EVER INCREASING GREEN CONCEPT(32,1)|EVER INCREASING REGULATION(32,1)|CHLORINE CONTENT(31,5)|SOLID SAMPLE AOX CONTENT(30,1)|CHLORINE(28,1)|HARM(28,1)|MAMMAL(27,1)|COMBUSTION(26,6)|FILTER CUP(26,5)|CRUSHER(25,4)|ACTIVATED CARBON ADSORPTION(24,1)|DEATH(24,1)|OMEGA CM(24,1)|BOTTLE STOPPER(23,5)|SCISSORS(23,4)|CRUSHING(23,1)|GRANULARITY(21,2)|PAPER PULP(20,1)|FLASK(18,8)|OSCILLATOR SUPPORT PLATE(18,5)|NATURAL WATER(18,2)|PAPER INDUSTRY(17,1)|ULTRAPURE WATER(16,6)|FILTER CAKE(16,5)|MICROCOULOMB METER(16,3)|DRINKING WATER(16,1)|FATTY ACID(16,1)|ORGANIC CHLORIDE(14,9)|HYDROGEN CHLORIDE(13,3)|DOMESTIC GARBAGE(13,2)|OSCILLATION ADSORPTION TIME(13,1)|RED FUMING NITRIC ACID(11,7)|AOX CONTENT DETECTION(11,3)|WASHING LIQUID(11,3)|ACTIVATED CARBON(10,4)|STOCK SOLUTION(9,9)|FLASK2SO3SHAKING(9,3)|SEPARATED TEXTILE FABRIC(9,2)|IODINE VALUE(9,1)|MANDATORY EXECUTION INDEX(9,1)|WOOL DEGREASING(9,1)|ARTIFICIAL POLLUTION(8,1)|INORGANIC CHLORINE INTERFERENCE(8,1)|INSTABILITY DEFECT(8,1)|DETECTING AOX(7,2)|ACTIVE CARBON(6,4)|SAMPLE SEPARATION(6,4)|INVENTION2SO3THE(6,1)|ORGANISM PATHOLOGICAL CHANGE(6,1)|PERSISTENT ORGANIC POLLUTANT(6,1)|TEXTILE SAMPLE(5,4)|ABSORB HYDROGEN CHLORIDE(5,2)|CONTAMINATION(5,2)|TWEEZER(5,2)|AOX DETECTION(5,1)|GROUND POWDER(5,1)|INORGANIC CHLORIDE(5,1)|ION CHROMATOGRAPHY(5,1)|LIPOPHILICITY(5,1)|POTENTIOMETRIC TITRATION(5,1)|NITRIC ACID SODIUM SALT(4,17)|CUP(4,3)|PRESSURE FILTER(4,3)|ACETIC ACID ELECTROLYTE(4,1)|CARCINOGENESIS(4,1)| (CN104865306)|1. A detection method for adsorbable organic chloride in a solid sample is characterized by comprising the following steps: the method comprises the following steps:|a. crushing a solid sample into powder of 60-100 meshes by using a crusher or scissors and other tools, and weighing 10-50 mg of powder into a conical flask with a ground stopper;|b. 100ml of ultrapure water was added to the flask, and 5ml of Na was added2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|c. adding 50mg of activated carbon into the conical flask, plugging the bottle stopper tightly, placing the conical flask on an oscillator support plate, and oscillating and adsorbing for more than 6 hours;|d. filtering the liquid in the conical flask by using a quartz filter bowl, washing the conical flask and the filter by 25mL of sodium nitrate washing liquid in a grading way, and finally washing by using a small amount of water;|e. putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|f. and (3) absorbing hydrogen chloride generated by combustion by adopting electrolyte, and measuring the chlorine content in the electrolyte by using a micro coulometer to obtain the AOX content in the solid sample.|2. The method for detecting the adsorbable organic chloride in the solid sample according to claim 1, wherein: the properties of the active carbon are that the iodine value is more than or equal to 1050, the chloride is less than 0.0015 percent, and the granularity is about 50 mu m; the conductivity resistivity of the ultrapure water is greater than 15M omega cm; the oscillation adsorption time is more than 6 h; the temperature of the combustion furnace is 1000 +/-10 ℃. (CN104865306)|TECHNICAL FIELD|[0002] The invention belongs to the measurement technology, and particularly relates to a method for detecting adsorbable organic chloride in a solid sample.|BACKGROUND ART|[0004] Most of organic chlorides are persistent organic pollutants, are not generally present in natural water bodies, are signs of artificial pollution, and have been paid attention to all the time, wherein most of the organic chlorides (AOX) can be adsorbed, and the organic chlorides, bromides and iodides are not included. AOX has strong lipophilicity, is not easy to degrade in natural water, is easy to deposit on fat parts of cell tissues, has strong toxicity, is easy to cause pathological changes of organisms, and can cause carcinogenesis, teratogenicity, mutation and the like. With the increasing environmental pollution of industrial processes, the organic halide characterized by AOX has become an international water quality index, and the limit value is regulated.|[0005] AOX is produced by many industries. The AOX pollution of the paper industry is mainly derived from chlorine bleaching wastewater, and researches show that during the chlorine bleaching process of paper pulp, more than 500 organic chlorides such as trichloromethane, chlorinated phenols, chlorinated fatty acids and the like can be generated, the organic chlorides can cause diseases or death to biological accumulation when discharged into natural water, and can directly act on mammals and human beings through drinking water, and the harm is very large. The discharge standard of water pollution of pulping and paper making industry (GB3544-2008) lists AOX as a mandatory execution index, and the discharge limit value is 12 mg/L. Wool degreasing agents, insecticides, dry cleaning agents, bleaching agents and the like which are common in dyeing and finishing processing of the textile industry in China are all organic halides, and the organic chlorides can be left or generated by secondary reaction in the using process. These organic chlorides remain on the clothes, and are very likely to cause harm to human health. Meanwhile, the discharge of industrial three wastes can bring serious pollution to the environment. Pesticides, preservatives and the like used in the industries of agriculture, pasture and forestry and the like can bring more AOX. The domestic garbage also contains a large amount of AOX, and if the domestic garbage is not properly treated, secondary pollution is caused.|[0006] The current methods for detecting AOX include ' determination of water quality-adsorbable organic halogen (AOX) ' -microcoulomb method ' (GB/T15959. 1995) and ' determination of water quality-adsorbable organic halogen (AOX) ' -ion chromatography (HJ/T83-2001), which are internationally recognized, but the two methods are both directed at the detection of the content of AOX in water. The studies on AOX in solid samples were: the content of AOX in the soil is analyzed by the microcoulomb method, but the treatment time is short and the errors exist. The content of 3 organic chlorides is analyzed by adopting gas chromatography-mass spectrometry, but the treatment is complicated, and the weight cannot be measured. Other methods include an electrode method, a potentiometric titration method, a neutron activation method and the like, and have the defects of instability, easy interference, high cost and the like. For AOX detection in a solid sample, special pretreatment is needed, organic chloride is adsorbed by activated carbon, inorganic chloride in the solid is washed away, and otherwise, the error is large. Therefore, in view of the hazard of AOX, there is a need to establish a unified detection method for AOX content in solid sample to adapt to the ever-increasing regulations and the ever-increasing green concept.|DISCLOSURE|[0007] Disclosure of Invention|[0008] The invention aims to provide a method for detecting adsorbable organic chloride in a solid sample, which is simple, convenient, accurate, reliable and low in cost.|[0009] The technical scheme of the invention comprises the following specific steps:|[0010] 1. crushing a solid sample into powder of 60-100 meshes by using a crusher or scissors and other tools, and weighing 10-50 mg of powder into a conical flask with a ground stopper;|[0011] 2. to the flask was added 100mL of ultrapure water, and 5mL of Na was added2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|[0012] 3. adding 50mg of activated carbon into the conical flask, plugging the bottle stopper tightly, placing the conical flask on an oscillator support plate, and oscillating and adsorbing for more than 6 hours;|[0013] 4. filtering the liquid in the conical flask by using a quartz filter bowl, washing the conical flask and the filter by 25mL of sodium nitrate washing liquid in a grading way, and finally washing by using a small amount of water;|[0014] 5. putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|[0015] 6. and (3) absorbing hydrogen chloride generated by combustion by adopting electrolyte, and measuring the chlorine content in the electrolyte by using a micro coulometer to obtain the AOX content in the solid sample.|[0016] Na according to the invention2SO3The concentration is 0.2 mol/L;|[0017] the preparation method of the sodium nitrate stock solution comprises the steps of weighing 17g of sodium nitrate, dissolving the sodium nitrate in water, adding 1.4mL of concentrated nitric acid, and transferring the solution into a 1000mL volumetric flask for constant volume;|[0018] the activated carbon of the invention is required to have a typical value of more than or equal to 1050, less than 0.0015% of chloride and a granularity of about 50 mu m;|[0019] the preparation method of the sodium nitrate washing liquid comprises the steps of taking 50mL of sodium nitrate stock solution, transferring the sodium nitrate stock solution into a 1000mL volumetric flask, and diluting the sodium nitrate stock solution to a scale with water.|[0020] The electrolyte is acetic acid electrolyte, and the preparation method comprises the steps of measuring 70mL of glacial acetic acid, adding 30mL of distilled water, and uniformly mixing.|[0021] The invention has the following advantages:|[0022] 1. the detection sample is a solid sample, and a detection method is provided for detecting AOX in the solid.|[0023] 2. The method has high precision, and can eliminate interference of inorganic chlorine.|INVENTION MODE|[0024] Detailed Description|[0025] The following description further illustrates the present invention in detail with reference to specific examples, but the present invention is not limited to these examples.|INVENTION MODE|[0026] EXAMPLE 1 detection of AOX content in soil|[0027] Crushing a soil sample into powder with the particle size of less than 60 meshes by using a pulverizer, and taking a proper amount of powder to analyze the moisture content of the powder;|[0028] 50mg of soil powder was accurately weighed in a flask with a ground stopper, and 100mL of ultrapure water and 5mL of Na were added to the flask2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|[0029] adding 50mg of active carbon into the conical flask, plugging a bottle stopper, placing the conical flask on an oscillator support plate, adjusting the frequency of the oscillator to be 150r/min, and oscillating and adsorbing for 8 hours;|[0030] filtering the liquid in the conical flask by using a quartz filter cup and a pressure filter device, and adjusting N2The pressure was 0.25MPa and the flask and filter were washed in portions with 25mL of sodium nitrate wash, finally with a small amount of water and with N2Blowing off for 5 min;|[0031] putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|[0032] and (3) absorbing hydrogen chloride generated by combustion by using electrolyte, and measuring the chlorine content in the electrolyte by using a microcoulomb meter to obtain the AOX content of 27.48mg/kg in the soil sample.|INVENTION MODE|[0033] Example 2 detection of AOX content in textiles|[0034] Separating the textile sample into single thread-shaped or velvet-shaped by using scissors and tweezers, crushing the textile sample into powder of 60-100 meshes by using a crusher, and taking a proper amount of separated sample to analyze the moisture content of the separated sample;|[0035] another 30mg portion of the separated textile fabric was accurately weighed into a flask with a ground stopper, and 100mL of ultrapure water and 5mL of Na were added to the flask2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|[0036] adding 50mg of active carbon into the conical flask, plugging a bottle stopper, placing the conical flask on an oscillator support plate, adjusting the frequency of the oscillator to be 150r/min, and oscillating and adsorbing for 6 hours;|[0037] filtering the liquid in the conical flask by using a quartz filter cup and a pressure filter device, and adjusting N2The pressure was 0.25MPa and the flask and filter were washed in portions with 25mL of sodium nitrate wash, finally with a small amount of water and with N2Blowing off for 5 min;|[0038] putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|[0039] the electrolyte is adopted to absorb hydrogen chloride generated by combustion, and the chlorine content in the electrolyte is measured by a microcoulomb meter, so that the AOX content in the textile sample is 130.12 mg/kg.|INVENTION MODE|[0040] EXAMPLE 3 detection of AOX content in paper|[0041] Separating the paper sample into small pieces by using scissors and tweezers, crushing the small pieces into powder of 60-100 meshes by using a crusher, and taking a proper amount of separated sample to analyze the water content of the separated sample;|[0042] another 50mg portion of the separated textile fabric was accurately weighed into a flask with a ground stopper, and 100mL of ultrapure water and 5mL of Na were added to the flask2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|[0043] adding 50mg of active carbon into the conical flask, plugging a bottle stopper, placing the conical flask on an oscillator support plate, adjusting the frequency of the oscillator to be 150r/min, and carrying out oscillation adsorption for 7 hours;|[0044] filtering the liquid in the conical flask by using a quartz filter cup and a pressure filter device, and adjusting N2The pressure was 0.25MPa and the flask and filter were washed in portions with 25mL of sodium nitrate wash, finally with a small amount of water and with N2Blowing off for 5 min;|[0045] putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|[0046] the electrolyte is adopted to absorb hydrogen chloride generated by combustion, and the chlorine content in the electrolyte is measured by a microcoulomb meter, so that the AOX content in the textile sample is 567.52 mg/kg. (CN104865306)|TECHNICAL FIELD|[0002] The invention belongs to the measurement technology, and particularly relates to a method for detecting adsorbable organic chloride in a solid sample.|BACKGROUND ART|[0004] Most of organic chlorides are persistent organic pollutants, are not generally present in natural water bodies, are signs of artificial pollution, and have been paid attention to all the time, wherein most of the organic chlorides (AOX) can be adsorbed, and the organic chlorides, bromides and iodides are not included. AOX has strong lipophilicity, is not easy to degrade in natural water, is easy to deposit on fat parts of cell tissues, has strong toxicity, is easy to cause pathological changes of organisms, and can cause carcinogenesis, teratogenicity, mutation and the like. With the increasing environmental pollution of industrial processes, the organic halide characterized by AOX has become an international water quality index, and the limit value is regulated.|[0005] AOX is produced by many industries. The AOX pollution of the paper industry is mainly derived from chlorine bleaching wastewater, and researches show that during the chlorine bleaching process of paper pulp, more than 500 organic chlorides such as trichloromethane, chlorinated phenols, chlorinated fatty acids and the like can be generated, the organic chlorides can cause diseases or death to biological accumulation when discharged into natural water, and can directly act on mammals and human beings through drinking water, and the harm is very large. The discharge standard of water pollution of pulping and paper making industry (GB3544-2008) lists AOX as a mandatory execution index, and the discharge limit value is 12 mg/L. Wool degreasing agents, insecticides, dry cleaning agents, bleaching agents and the like which are common in dyeing and finishing processing of the textile industry in China are all organic halides, and the organic chlorides can be left or generated by secondary reaction in the using process. These organic chlorides remain on the clothes, and are very likely to cause harm to human health. Meanwhile, the discharge of industrial three wastes can bring serious pollution to the environment. Pesticides, preservatives and the like used in the industries of agriculture, pasture and forestry and the like can bring more AOX. The domestic garbage also contains a large amount of AOX, and if the domestic garbage is not properly treated, secondary pollution is caused.|[0006] The current methods for detecting AOX include ' determination of water quality-adsorbable organic halogen (AOX) ' -microcoulomb method ' (GB/T15959. 1995) and ' determination of water quality-adsorbable organic halogen (AOX) ' -ion chromatography (HJ/T83-2001), which are internationally recognized, but the two methods are both directed at the detection of the content of AOX in water. The studies on AOX in solid samples were: the content of AOX in the soil is analyzed by the microcoulomb method, but the treatment time is short and the errors exist. The content of 3 organic chlorides is analyzed by adopting gas chromatography-mass spectrometry, but the treatment is complicated, and the weight cannot be measured. Other methods include an electrode method, a potentiometric titration method, a neutron activation method and the like, and have the defects of instability, easy interference, high cost and the like. For AOX detection in a solid sample, special pretreatment is needed, organic chloride is adsorbed by activated carbon, inorganic chloride in the solid is washed away, and otherwise, the error is large. Therefore, in view of the hazard of AOX, there is a need to establish a unified detection method for AOX content in solid sample to adapt to the ever-increasing regulations and the ever-increasing green concept.|DISCLOSURE|[0007] Disclosure of Invention|[0008] The invention aims to provide a method for detecting adsorbable organic chloride in a solid sample, which is simple, convenient, accurate, reliable and low in cost.|[0009] The technical scheme of the invention comprises the following specific steps:|[0010] 1. crushing a solid sample into powder of 60-100 meshes by using a crusher or scissors and other tools, and weighing 10-50 mg of powder into a conical flask with a ground stopper;|[0011] 2. to the flask was added 100mL of ultrapure water, and 5mL of Na was added2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|[0012] 3. adding 50mg of activated carbon into the conical flask, plugging the bottle stopper tightly, placing the conical flask on an oscillator support plate, and oscillating and adsorbing for more than 6 hours;|[0013] 4. filtering the liquid in the conical flask by using a quartz filter bowl, washing the conical flask and the filter by 25mL of sodium nitrate washing liquid in a grading way, and finally washing by using a small amount of water;|[0014] 5. putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|[0015] 6. and (3) absorbing hydrogen chloride generated by combustion by adopting electrolyte, and measuring the chlorine content in the electrolyte by using a micro coulometer to obtain the AOX content in the solid sample.|[0016] Na according to the invention2SO3The concentration is 0.2 mol/L;|[0017] the preparation method of the sodium nitrate stock solution comprises the steps of weighing 17g of sodium nitrate, dissolving the sodium nitrate in water, adding 1.4mL of concentrated nitric acid, and transferring the solution into a 1000mL volumetric flask for constant volume;|[0018] the activated carbon of the invention is required to have a typical value of more than or equal to 1050, less than 0.0015% of chloride and a granularity of about 50 mu m;|[0019] the preparation method of the sodium nitrate washing liquid comprises the steps of taking 50mL of sodium nitrate stock solution, transferring the sodium nitrate stock solution into a 1000mL volumetric flask, and diluting the sodium nitrate stock solution to a scale with water.|[0020] The electrolyte is acetic acid electrolyte, and the preparation method comprises the steps of measuring 70mL of glacial acetic acid, adding 30mL of distilled water, and uniformly mixing.|[0021] The invention has the following advantages:|[0022] 1. the detection sample is a solid sample, and a detection method is provided for detecting AOX in the solid.|[0023] 2. The method has high precision, and can eliminate interference of inorganic chlorine.|INVENTION MODE|[0024] Detailed Description|[0025] The following description further illustrates the present invention in detail with reference to specific examples, but the present invention is not limited to these examples.|INVENTION MODE|[0026] EXAMPLE 1 detection of AOX content in soil|[0027] Crushing a soil sample into powder with the particle size of less than 60 meshes by using a pulverizer, and taking a proper amount of powder to analyze the moisture content of the powder;|[0028] 50mg of soil powder was accurately weighed in a flask with a ground stopper, and 100mL of ultrapure water and 5mL of Na were added to the flask2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|[0029] adding 50mg of active carbon into the conical flask, plugging a bottle stopper, placing the conical flask on an oscillator support plate, adjusting the frequency of the oscillator to be 150r/min, and oscillating and adsorbing for 8 hours;|[0030] filtering the liquid in the conical flask by using a quartz filter cup and a pressure filter device, and adjusting N2The pressure was 0.25MPa and the flask and filter were washed in portions with 25mL of sodium nitrate wash, finally with a small amount of water and with N2Blowing off for 5 min;|[0031] putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|[0032] and (3) absorbing hydrogen chloride generated by combustion by using electrolyte, and measuring the chlorine content in the electrolyte by using a microcoulomb meter to obtain the AOX content of 27.48mg/kg in the soil sample.|INVENTION MODE|[0033] Example 2 detection of AOX content in textiles|[0034] Separating the textile sample into single thread-shaped or velvet-shaped by using scissors and tweezers, crushing the textile sample into powder of 60-100 meshes by using a crusher, and taking a proper amount of separated sample to analyze the moisture content of the separated sample;|[0035] another 30mg portion of the separated textile fabric was accurately weighed into a flask with a ground stopper, and 100mL of ultrapure water and 5mL of Na were added to the flask2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|[0036] adding 50mg of active carbon into the conical flask, plugging a bottle stopper, placing the conical flask on an oscillator support plate, adjusting the frequency of the oscillator to be 150r/min, and oscillating and adsorbing for 6 hours;|[0037] filtering the liquid in the conical flask by using a quartz filter cup and a pressure filter device, and adjusting N2The pressure was 0.25MPa and the flask and filter were washed in portions with 25mL of sodium nitrate wash, finally with a small amount of water and with N2Blowing off for 5 min;|[0038] putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|[0039] the electrolyte is adopted to absorb hydrogen chloride generated by combustion, and the chlorine content in the electrolyte is measured by a microcoulomb meter, so that the AOX content in the textile sample is 130.12 mg/kg.|INVENTION MODE|[0040] EXAMPLE 3 detection of AOX content in paper|[0041] Separating the paper sample into small pieces by using scissors and tweezers, crushing the small pieces into powder of 60-100 meshes by using a crusher, and taking a proper amount of separated sample to analyze the water content of the separated sample;|[0042] another 50mg portion of the separated textile fabric was accurately weighed into a flask with a ground stopper, and 100mL of ultrapure water and 5mL of Na were added to the flask2SO3Shaking up, adjusting the pH to be less than 2 by using concentrated nitric acid, and continuously adding 5mL of sodium nitrate stock solution;|[0043] adding 50mg of active carbon into the conical flask, plugging a bottle stopper, placing the conical flask on an oscillator support plate, adjusting the frequency of the oscillator to be 150r/min, and carrying out oscillation adsorption for 7 hours;|[0044] filtering the liquid in the conical flask by using a quartz filter cup and a pressure filter device, and adjusting N2The pressure was 0.25MPa and the flask and filter were washed in portions with 25mL of sodium nitrate wash, finally with a small amount of water and with N2Blowing off for 5 min;|[0045] putting the filtered quartz filter cup and the filter cake into a quartz boat, and feeding the quartz boat into a combustion furnace at 1000 ℃;|[0046] the electrolyte is adopted to absorb hydrogen chloride generated by combustion, and the chlorine content in the electrolyte is measured by a microcoulomb meter, so that the AOX content in the textile sample is 567.52 mg/kg. Family Number|(70706682)|70706682|Abstract|(CN104865306 A)|The invention discloses a detection method of adsorbable organic chlorides in a solid sample , belongs to the measurement technology , and can solve the problem of detection of content of adsorbable organic chloride in the solid sample . According to the method , the solid sample is treated by crushing , adsorbing with activated carbon , removal of inorganic chlorine with nitrate and nitric acid , filtering , burning at 1000 DEG C , micro coulomb titration and other steps , and the content of AOX ( absorbable organic halogen ) content in the solid sample can be calculated . According to the method , the influence of the inorganic chloride can be fully eliminated , and the content of the AOX ( absorbable organic halogen ) content in the solid sample can be accurately analyzed . |IPC codes|(CN104865306 A)|G01N - 027/42 | Measurement G01N-027/42 G01N-027/42 CN112505204|CN113848244|CN112946166|CN107976477|CN113376307|CN109283024|CN108982750|WO2018218960|CN108535348|CN108362814 CN112505204 93141505 WHO=Examiner SELF=N CAT=Y CAT=X|CN113848244 97929514 WHO=Examiner SELF=N CAT=Y|CN112946166 94677056 WHO=Examiner SELF=N CAT=Y|CN107976477 79540449 WHO=Examiner SELF=N CAT=Y|CN113376307 96040978 WHO=Examiner SELF=N CAT=A|CN109283024 83230208 WHO=Examiner SELF=N CAT=A|CN108982750 82456386 WHO=Examiner SELF=N CAT=A|WO2018218960 78883674 WHO=Examiner SELF=N CAT=A|CN108535348 81316150 WHO=Examiner SELF=N CAT=A|CN108362814 80796138 WHO=Examiner SELF=N CAT=A CN103969316|CN103517974|CN101290303|CN1756945|DE10321357|CN87214257U CN103969316 67173427 WHO=Examiner SELF=N CAT=A|CN103517974 62251212 WHO=Examiner SELF=N CAT=A|CN101290303 62149385 WHO=Examiner SELF=N CAT=A|CN1756945 107390364 WHO=Examiner SELF=N CAT=A|DE10321357 13575730 WHO=Examiner SELF=N CAT=A|CN87214257U 6333320 WHO=Examiner SELF=N CAT=A 胡雄星 等: &quot;微库仑法测定固体样品中的可吸附有机卤化物&quot;, 《分析试验室》 (Cat. Y)|邢耀宇: &quot;纺织品中有机氯化合物离子色谱检测方法研究&quot;, 《中国优秀硕士学位论文全文数据库工程科技I辑》 (Cat. Y) CN87214257U; DE10321357; CN1756945; CN101290303; CN103517974; CN103969316 LAPSED (CN104865306)|LAPSED DEAD (CN104865306)|DEAD (CN104865306)|LEGAL DETAILS FOR CN104865306|Actual or expected expiration date=2018-03-16|Legal state=DEAD|Status=LAPSED|Event publication date=2015-04-23|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201510198643|Application date=2015-04-23|Standardized application number=2015CN-0198643|Event publication date=2015-08-26|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN104865306|Publication stage code=A|Publication date=2015-08-26|Standardized publication number=CN104865306|Event publication date=2015-08-26|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2015-09-23|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2018-03-16|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjlFEeW/kQ/K3lfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=qJhWoKyGlPzz0jlmgCkkUZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN104865306)|NAME=ZHANG SHENGYOU|NAME=SU ZHENHUA|NAME=CAO YINGGE|NAME=ZHANG YU|NAME=FENG WENYING|NAME=LIANG FANGYUAN 0 1 Titre: (CN104865306)|Detection method of adsorbable organic chlorides in solid sample Résumé: (CN104865306)|The invention discloses a detection method of adsorbable organic chlorides in a solid sample, belongs to the measurement technology, and can solve the problem of detection of content of adsorbable organic chloride in the solid sample. According to the method, the solid sample is treated by crushing, adsorbing with activated carbon, removal of inorganic chlorine with nitrate and nitric acid, filtering, burning at 1000 DEG C, micro coulomb titration and other steps, and the content of AOX (absorbable organic halogen) content in the solid sample can be calculated. According to the method, the influence of the inorganic chloride can be fully eliminated, and the content of the AOX (absorbable organic halogen) content in the solid sample can be accurately analyzed. 104 Abstract gpt-4o-mini no The article focuses on a detection method for organic chlorides in solid samples and does not relate to accelerated weathering or CO₂ capture.
105 CN202411750435 CN202411750435 CN119800102 114163661 CN119800102 A 2025-04-11 [CN119800102] 2024-12-02 2024-12-02 2025-04-11 (CN119800102)|2044-12-02 (CN119800102)|Method for extracting lithium from electrolytic aluminum waste through mechanical strengthening and mechanical strengthening leaching kettle (CN119800102)|The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for extracting lithium from electrolytic aluminum waste through mechanical strengthening and a mechanical strengthening leaching kettle. The method comprises the following steps: (1) coarsely crushing the electrolytic aluminum waste; (2) calcining or combusting the electrolytic aluminum waste to remove carbon; (3) after carbon removal, the electrolytic aluminum waste is subjected to mechanical strengthening, and lithium is selectively leached by controlling the leaching acidity; (4) performing two-stage impurity removal on the lithium leachate; and (5) concentrating and denitrifying the impurity-removed liquid, precipitating lithium, carbonizing and crystallizing to prepare the battery-grade lithium carbonate. According to the method, carbon in the electrolytic aluminum waste is removed through a calcination or combustion method, leaching of lithium is strengthened through a mechanical strengthening method, meanwhile, the leaching condition is controlled to enable lithium in the waste aluminum slag to be dissolved out into a leaching solution, and aluminum, iron, sodium and most fluorine in the waste aluminum slag are not dissolved out and left in the leaching slag. And performing simple impurity removal, concentration and denitration on the leachate to prepare the battery-grade lithium carbonate. The method is simple in process and high in lithium extraction rate, and cryolite is mainly contained in leaching residues and can be utilized subsequently. JINCHUAN|LANZHOU JINCHUAN SCIENCE PARK (CN119800102)|JINCHUAN GROUP CO. LTD. ([CN])|LANZHOU JINCHUAN SCIENCE PARK CO LTD CHAI GENFENG|BAI YANLI|YANG XIAOYAN|WANG JUANHUI|CHEN TIANYI|WANG QIAN|SONG FANG|YAN XIANYONG (CN119800102)|CHAI GENFENG|BAI YANLI|YANG XIAOYAN|WANG JUANHUI|CHEN TIANYI|WANG QIAN|SONG FANG|YAN XIANYONG (CN119800102)|LI ZIJIAN;CHINA NONFERROUS METALS INDUSTRY PATENT CENTER|Reg. Nb: 11028 (CN119800102)|Compared with the prior art, the invention has the following advantages:|Therefore, there is a need to develop a simpler, economical and efficient method for extracting lithium from electrolytic aluminum slag to solve the above problems.|According to the invention, the lithium sodium cryolite in the refractory electrolytic aluminum waste residue is dissolved by adopting the aluminum salt solution, so that lithium in the refractory electrolytic aluminum waste residue can be converted into lithium chloride or lithium sulfate, the lithium leaching rate in the refractory electrolytic aluminum waste residue is improved, and the problems of lower lithium leaching rate and environmental friendliness in the existing recovery process are effectively solved.|In the second-stage impurity removal process, oxalic acid is used as a calcium remover instead of conventional ion exchange resin, so that excessive waste water is avoided, the problem that the ion exchange resin is easy to scale in a sulfuric acid system is avoided, and the calcium remover can remove calcium efficiently and the system operates smoothly.| (CN119800102)|1. A mechanical strengthening leaching kettle is characterized by comprising a kettle body, a jacket, a tank cover, a liquid adding port, a stirring device and grinding balls, wherein the jacket is coated on the outer side of the kettle body, a heating pipe is arranged in the jacket, the tank cover is positioned above the kettle body, the liquid adding port is arranged on the tank cover, the stirring device comprises a motor, a speed reducer, a stirring shaft and a stirring paddle on the outer side of the stirring shaft, the motor and the speed reducer are positioned on the tank cover, the stirring shaft is connected with the motor and the speed reducer, the stirring shaft and the stirring paddle are positioned in the kettle body, the grinding balls are arranged in the kettle body, and the grinding balls are zirconia balls.|2. The method for mechanically strengthening and extracting lithium from the electrolytic aluminum waste is characterized by comprising the following steps of: step 1, crushing electrolytic aluminum waste with carbon content more than 45% and aluminum content more than 10 times of lithium content; Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and coarsely grinding to a granularity of 1-5mm to obtain a carbon-removed material; step 3, carrying out mechanical strengthening acid leaching on the carbon-removed material, namely carrying out fine grinding and selective leaching on the carbon-removed material in a mechanical strengthening leaching kettle provided with grinding balls, adjusting the leaching pH value to 3.0-4.0, and filtering to obtain leaching liquid and leaching slag; Step 4, performing two-stage impurity removal, wherein the first stage impurity removal process comprises the steps of adding an oxidant into the leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues; Step 5, heating and concentrating the filtrate containing lithium, and then freezing and crystallizing to obtain a denitration liquid; Step 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate; And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. | (CN119800102)|The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for extracting lithium from electrolytic aluminum waste by mechanical reinforcement and a mechanical reinforcement leaching kettle.| (CN119800102)|1. A mechanical strengthening leaching kettle is characterized by comprising a kettle body, a jacket, a tank cover, a liquid adding port, a stirring device and grinding balls, wherein the jacket is coated on the outer side of the kettle body, a heating pipe is arranged in the jacket, the tank cover is positioned above the kettle body, the liquid adding port is arranged on the tank cover, the stirring device comprises a motor, a speed reducer, a stirring shaft and a stirring paddle on the outer side of the stirring shaft, the motor and the speed reducer are positioned on the tank cover, the stirring shaft is connected with the motor and the speed reducer, the stirring shaft and the stirring paddle are positioned in the kettle body, the grinding balls are arranged in the kettle body, and the grinding balls are zirconia balls.|2. The method for mechanically strengthening and extracting lithium from the electrolytic aluminum waste is characterized by comprising the following steps of:| step 1, crushing electrolytic aluminum waste with carbon content more than 45% and aluminum content more than 10 times of lithium content; | Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and coarsely grinding to a granularity of 1-5mm to obtain a carbon-removed material; | step 3, carrying out mechanical strengthening acid leaching on the carbon-removed material, namely carrying out fine grinding and selective leaching on the carbon-removed material in a mechanical strengthening leaching kettle provided with grinding balls, adjusting the leaching pH value to 3.0-4.0, and filtering to obtain leaching liquid and leaching slag; | Step 4, performing two-stage impurity removal, wherein the first stage impurity removal process comprises the steps of adding an oxidant into the leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues; | Step 5, heating and concentrating the filtrate containing lithium, and then freezing and crystallizing to obtain a denitration liquid; | Step 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate; | And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. |3. The method for mechanically strengthening and extracting lithium from the electrolytic aluminum waste according to claim 2, wherein the electrolytic aluminum waste in the step 1 comprises 1% -1.1% of lithium, 12.2% -13.0% of aluminum, 11.0% -12.0% of sodium, 0.8% -0.9% of iron, 1.5% -2.0% of calcium, 0.24% -0.26% of magnesium, 0.1% of silicon, 13.0% -13.5% of fluorine, 0.14% -0.15% of sulfur, 0.1% of manganese, 45% of carbon and the balance of water.|4. The method for mechanically strengthening and extracting lithium from electrolytic aluminum scraps according to claim 2, wherein the material is the crushed electrolytic aluminum scraps in the step 1, and the size of the crushed electrolytic aluminum scraps is 1-10cm.|5. The method for mechanically strengthening and extracting lithium from electrolytic aluminum waste according to claim 2, wherein the slurry liquid-solid ratio of water to carbon removal material in the leaching process in the step 3 is 3-5:1, the mass ratio of the carbon removal material to grinding balls is 1:1-1.5, the leaching agent is 98% sulfuric acid, the leaching temperature is 60-90 ℃, and the leaching time is 1-3h.|6. The method for mechanically strengthening and extracting lithium from electrolytic aluminum waste according to claim 2, wherein the oxidant in the first stage of impurity removal in the step 4 is hydrogen peroxide, sodium chlorate, sodium hypochlorite, chlorine, air and oxygen, the impurity removal temperature is 55-70 ℃, alkali is sodium hydroxide solution with mass concentration of 5-20%, the reaction time is 1-5h, the reaction time in the second stage of impurity removal is 1-5h, the calcium remover is oxalic acid, and the amount of the added calcium remover is 0.05% -0.1% of the electrolytic aluminum waste.|7. The method for mechanically strengthening and extracting lithium from electrolytic aluminum scraps according to claim 2, wherein the freezing crystallization temperature in the step 5 is-10 ℃ to 10 ℃.|8. The method for mechanically strengthening and extracting lithium from electrolytic aluminum scraps according to claim 2, wherein the heating temperature in the step 6 is 90-100 ℃.|9. The method for mechanically strengthening and extracting lithium from electrolytic aluminum waste according to claim 2, wherein the mass ratio of pure water to crude lithium carbonate in the step 7 is 9-10:1, and the pressure of the introduced CO 2 gas is 0.1-0.2MPa.|10. The method for mechanically strengthening and extracting lithium from electrolytic aluminum scraps according to claim 2, wherein the temperature of the heating crystallization in the step 7 is 90-100 ℃. (CN119800102)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for extracting lithium from electrolytic aluminum waste by mechanical reinforcement and a mechanical reinforcement leaching kettle.|BACKGROUND ART|[0002] In recent years, the country has brought out a series of policies to the new energy and energy storage industry to encourage development, and a plurality of leading enterprises such as Ningde times, BI, guo Xuan Gao and the like in the industry lead the new energy industry of China to go forward in the world, and the development of the new energy industry simultaneously drives the layout of lithium resources and the development and continuous progress of lithium extraction technology.|[0003] The electrolytic aluminum industry forms an aluminum production system in China aluminum industry, guangxi apple aluminum industry, south flat aluminum industry and the like, the quantity and the scale of enterprises are continuously increased along with the economic development, the yield of electrolytic aluminum waste residues is continuously increased, the electrolytic aluminum waste residues contain a certain amount of lithium and cryolite, and due to the rising of the price of the lithium, a great deal of research is developed on the extraction and utilization technology of the lithium in the aluminum waste residues in recent years, and enterprises such as polyfluoro, xinjiang weapon groups and the like have industrialized layout, so that the lithium and aluminum resources can be greatly saved.|[0004] For example, china patent with the application number 2022113448491 discloses a method and equipment for recycling electrolytic aluminum waste residues, wherein the electrolytic aluminum waste residues are pulped with sulfuric acid for sulfating roasting, the roasted materials are hydrolyzed, alkali is added into the filtered solution for producing aluminum hydroxide precipitation, sodium carbonate is added into the filtrate for forming sodium sulfate, and the recycled hydrogen fluoride, aluminum hydroxide and sodium sulfate synthetic cryolite are sold to an electrolytic aluminum factory.|[0005] The Chinese patent with the application number 2023107040418 discloses a process method for improving the lithium leaching rate in refractory aluminum electrolysis waste residues, which comprises the following steps of preparing 10L of 5% aluminum trichloride solution, adding 10g of waste residues into every 100ml of aluminum trichloride solution, adding 1kg of waste residues together, controlling the final pH value to be 3, leaching at room temperature for 2 hours, filtering and washing the filter residues, wherein the filter residues mainly contain impurities such as carbon, and the filtrate enters a impurity removal enrichment purification process. According to the invention, the lithium sodium cryolite in the refractory electrolytic aluminum waste residue is dissolved by adopting the aluminum salt solution, so that lithium in the refractory electrolytic aluminum waste residue can be converted into lithium chloride or lithium sulfate, the lithium leaching rate in the refractory electrolytic aluminum waste residue is improved, and the problems of lower lithium leaching rate and environmental friendliness in the existing recovery process are effectively solved. According to the method, aluminum trichloride is used as a dissolution medium, the leaching solution contains extremely high aluminum content, and the recovery of lithium is affected although the leaching rate of lithium is relatively high.|[0006] In addition, aiming at the electrolytic aluminum waste residue with very high sodium and aluminum contents and nearly half of carbon, the amount of sulfuric acid and sodium hydroxide required for extracting all aluminum and lithium in the electrolytic aluminum waste residue is very large, the crystallization amount of sodium sulfate is large, the existence of carbon can cause large precipitation slag amount, the precipitation filtration property is poor, and the total recovery rate of lithium is affected. Therefore, there is a need to develop a simpler, economical and efficient method for extracting lithium from electrolytic aluminum slag to solve the above problems.|DISCLOSURE|Disclosure of Invention|[0007] Therefore, in order to solve the problems existing in the prior art, the invention provides a method for mechanically strengthening and extracting lithium from electrolytic aluminum waste and a mechanically strengthening leaching kettle, wherein the method selectively extracts lithium from waste aluminum slag by controlling leaching conditions, limits leaching of impurities such as aluminum, iron and the like in the slag, and further prepares lithium carbonate from lithium sulfate, and specifically comprises the following steps:|[0008] step 1, crushing electrolytic aluminum waste with carbon content more than 45% and aluminum content more than 10 times of lithium content; |[0009] Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and coarsely grinding to a granularity of 1-5mm to obtain a carbon-removed material; |[0010] Step 3, carrying out mechanical strengthening acid leaching on the carbon-removed material, namely carrying out fine grinding and selective leaching on the carbon-removed material in a mechanical strengthening leaching kettle, and filtering to obtain leaching liquid and leaching slag; |[0011] Step 4, performing two-stage impurity removal, wherein the first stage impurity removal process comprises the steps of adding an oxidant into the leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues; |[0012] Step 5, heating and concentrating the filtrate containing lithium, and then freezing and crystallizing to obtain a denitration liquid; |[0013] Step 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate; |[0014] And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. |[0015] Further, the electrolytic aluminum scraps in the step 1 comprise, by mass, 1% -1.1% of lithium, 12.2% -13.0% of aluminum, 11.0% -12.0% of sodium, 0.8% -0.9% of iron, 1.5% -2.0% of calcium, 0.24% -0.26% of magnesium, 0.1% of silicon, 13.0% -13.5% of fluorine, 0.14% -0.15% of sulfur, 0.1% of manganese, 45% of carbon and the balance of water.|[0016] Further, the size of the crushed electrolytic aluminum scraps in the step 1 is 1-10cm.|[0017] Further, in the step 3, the slurry liquid-solid ratio of water to the carbon removal material in the leaching process is 3-5:1, the mass ratio of the carbon removal material to the grinding balls is 1:1-1.5, the leaching agent is 98% sulfuric acid, the leaching temperature is 60-90 ℃, and the leaching time is 1-3 hours.|[0018] Further, the oxidant in the first stage of impurity removal in the step 4 is hydrogen peroxide, sodium chlorate, sodium hypochlorite, chlorine, air and oxygen, the impurity removal temperature is 55-70 ℃, alkali is sodium hydroxide solution with the mass concentration of 5-20%, the reaction time is 1-5h, the reaction time in the second stage of impurity removal is 1-5h, the calcium remover is oxalic acid, and the amount of the added calcium remover is 0.05% -0.1% of the electrolytic aluminum waste.|[0019] Further, the temperature of the freeze crystallization in the step 5 is-10 ℃ to 10 ℃.|[0020] Further, the heating temperature in step 6 is 90-100 ℃.|[0021] Further, in the step 7, the mass ratio of the pure water to the crude lithium carbonate is 9-10:1, and the pressure of the CO 2 gas is 0.1-0.2MPa.|[0022] Further, the temperature of the heating crystallization in the step 7 is 90-100 ℃.|[0023] The mechanical strengthening leaching kettle used in the step 3 comprises a kettle body, a jacket, a tank cover, a liquid adding port, a stirring device and grinding balls, wherein the jacket is coated on the outer side of the kettle body, a heating pipe is arranged in the jacket, the tank cover is positioned above the kettle body, the liquid adding port is arranged on the tank cover, the stirring device comprises a motor, a speed reducer, a stirring shaft and a stirring paddle on the outer side of the stirring shaft, the motor and the speed reducer are positioned on the tank cover, the stirring shaft is connected with the motor and the speed reducer, the stirring shaft and the stirring paddle are positioned in the kettle body, the grinding balls are arranged in the kettle body, and the grinding balls are zirconia balls.|[0024] Compared with the prior art, the invention has the following advantages:|[0025] (1) The electrolytic aluminum waste material is first calcined or burnt to eliminate most of carbon, and this can raise the lithium extracting capacity by almost one time, the concentration of lithium solution by about one time, lower the treating difficulty and cost and raise the lithium recovering rate and treating efficiency. |[0026] (2) According to the invention, by controlling the pH value in the leaching process to be 3.0-4.0, lithium in the electrolytic aluminum waste is dissolved out, most of aluminum, iron, sodium, fluorine and the like are not dissolved out and remain in leaching residues, so that the use amount of leaching acid is reduced, the use amount of impurity-removing alkali is greatly reduced, the residue filtering performance is good, the sodium content in the lithium solution after impurity removal is greatly reduced, the requirement can be met only by one-time denitration, the burden of each process is reduced, and the lithium extraction cost and the operation difficulty are reduced. Because the aluminum content in the material is very high, the lithium solution after impurity removal is relatively high in sodium content, and the leaching of aluminum is inhibited by controlling the acidity of the leaching solution, so that the loss of lithium caused by the fact that aluminum hydroxide is colloid during alkali addition and impurity removal is reduced.|[0027] (3) The invention adopts a mechanical strengthening method to strengthen leaching, solves the problems of high hardness and difficult fine grinding of the material, adopts a mechanical strengthening method to grind and leach simultaneously, increases the surface activity of the material and increases the active point of the material, thereby improving the treatment efficiency of electrolytic aluminum waste and the extraction rate of lithium, and the leaching rate of lithium can reach more than 95 percent, and has mild leaching condition and high treatment efficiency. The carbon in the leaching slag can be used as fuel, and most of the leaching slag is cryolite which can be used later.|[0028] (4) The lithium leaching solution is subjected to two-stage impurity removal, wherein the first stage impurity removal is performed to remove aluminum impurities, the second stage impurity removal is performed to remove other impurities such as iron, manganese, calcium and the like, and the two-stage impurity removal main products are different and are treated respectively. In the second-stage impurity removal process, oxalic acid is used as a calcium remover instead of conventional ion exchange resin, so that excessive waste water is avoided, the problem that the ion exchange resin is easy to scale in a sulfuric acid system is avoided, and the calcium remover can remove calcium efficiently and the system operates smoothly.|[0029] The method can effectively extract lithium in the electrolytic aluminum waste to prepare battery grade lithium carbonate, and the leaching slag mainly comprises cryolite, so that the method can be used and has good economic benefit.|DRAWINGS DESCRIPTION|[0030] Embodiments of the invention are further described below with reference to the accompanying drawings, in which:|[0031] FIG. 1 shows a process flow diagram of the present invention; |[0032] fig. 2 shows a cross-sectional view and a top view of the structure of the apparatus of the mechanically reinforced leaching tank. |[0033] The device comprises a 1-motor, a 2-speed reducer, a 3-tank cover, a 4-kettle body, a 5-stirring shaft, a 6-stirring paddle, a 7-jacket, an 8-grinding ball, a 9-heating pipe, a 10-valve, an 11-liquid adding port, a 12-hinge and 13-slurry.|INVENTION MODE|Detailed Description|[0034] In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail by the following examples with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0035] The mechanical strengthening leaching kettle comprises a kettle body 4, a jacket 7, a tank cover 3, a liquid adding opening 11, a stirring device and grinding balls 8, wherein the jacket 7 is coated on the outer side of the kettle body 4 and is internally provided with a heating pipe 9, the tank cover 3 is positioned above the kettle body 4, the tank cover 3 is provided with two liquid adding openings 11, the stirring device comprises a motor 1, a speed reducer 2, a stirring shaft 5 and stirring paddles 6 on the outer side of the stirring shaft, the motor 1 and the speed reducer 2 are positioned on the tank cover 3, the stirring shaft 5 is connected with the motor 1 and the speed reducer 2, the stirring shaft 5 and the stirring paddles 6 are positioned in the kettle body 4, a plurality of grinding balls 8 are arranged in the kettle body 4, and the grinding balls 8 are zirconia balls and are mixed with slurry 13. The outlet pipeline below the kettle body 4 is also provided with a valve 10, and when the slag amount of the system is small, filter cloth can be arranged on the lower pipeline for filtering. The tank cover 3 is a half-open tank cover and is divided into two parts, and the two parts are connected through a hinge 12 so as to realize half-open, so that the grinding balls can be conveniently placed and taken out.|[0036] A method for preparing battery grade lithium carbonate by electrolyzing aluminum scraps, which comprises the following steps:|[0037] the method comprises the steps of 1, crushing or manually crushing electrolytic aluminum waste with carbon content more than 45% and aluminum content more than 10 times of lithium content by a crusher, wherein the size of the crushed electrolytic aluminum waste is 1-10cm, the components and mass ratio of the electrolytic aluminum waste are respectively 1% -1.1% of lithium, 12.2-13.0% of aluminum, 11.0-12.0% of sodium, 0.8-0.9% of iron, 1.5-2.0% of calcium, 0.24-0.26% of magnesium, <0.1% of silicon, 13.0-13.5% of fluorine, 0.14-0.15% of sulfur, <0.1% of manganese, 45% of carbon and the balance of water. |[0038] Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and coarsely grinding to a granularity of 1-5mm to obtain a carbon-removed material;|[0039] and 3, carrying out mechanical strengthening acid leaching on the carbon-removed material, namely carrying out fine grinding and selective leaching on the carbon-removed material in a mechanical strengthening leaching kettle, regulating the leaching pH value to 3.0-4.0, filtering to obtain leaching liquid and leaching slag, washing the leaching slag twice, piling up the leaching slag after filtering, and returning the leaching slag washing water to leaching, wherein the slurry liquid-solid ratio of the carbon-removed material to water in the leaching process is 3-5:1, the mass ratio of the carbon-removed material to the grinding balls is 1:1-1.5, the leaching agent is 98% sulfuric acid, the leaching temperature is 60-90 ℃, and the leaching time is 1-3h. The leaching kettle is connected with an absorption device, and absorption liquid in the absorption device is dilute alkali liquid and absorbs fluorine and acid mist generated in the leaching process. |[0040] 2LiF+H2SO4→Li2SO4+2HF↑|[0041] 2Na3AlF6+6H2SO4→3Na2SO4+Al2(SO4)3+6HF↑|[0042] Fe+H2SO4→FeSO4+H2↑|[0043] Step 4, performing two-stage impurity removal, wherein the one-stage impurity removal process comprises the steps of adding an oxidant into the one-stage leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues, wherein the oxidant in the one-stage impurity removal process is hydrogen peroxide, sodium chlorate, sodium hypochlorite, chlorine, air and oxygen, the impurity removal temperature is 55-70 ℃, the alkali is sodium hydroxide solution with the mass concentration of 5-20%, and the reaction time is 1-5h;|[0044] 2FeSO4+H2SO4+H2O2→Fe2(SO4)3+2H2O( Chemical equation using hydrogen peroxide as oxidant |[0045] Al2(SO4)3+6NaOH→3Na2SO4+2Al(OH)3↓|[0046] Fe2(SO4)3+6NaOH→3Na2SO4+2Fe(OH)3↓|[0047] The second stage of impurity removing process is that adding calcium removing agent into filtrate, adding alkali to regulate pH value to 12.0-13.0, filtering to obtain lithium-containing filtrate and impurity filtering residue, and the reaction time in the second stage of impurity removing process is 1-5h, and the added calcium removing agent is 0.05% -0.1% of the electrolytic aluminum waste material.|[0048] Mn2++2NaOH→2Na++Mn(OH)2↓|[0049] H2C2O4+Ca2+→CaC2O4↓+2H+|[0050] Mg2++2NaOH→2Na++Mg(OH)2↓|[0051] And 5, heating and concentrating the filtrate containing lithium, and performing one-stage freezing crystallization to obtain a liquid after denitration, wherein the temperature of the freezing crystallization is between-10 ℃ and 10 ℃, and removing sodium sulfate.|[0052] And 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate, wherein the heating temperature is 90-100 ℃.|[0053] Li2SO4+Na2CO3→Li2CO3↓+2Na2SO4|[0054] And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. The mass ratio of the pure water to the crude lithium carbonate is 9-10:1, the pressure of the CO 2 gas is 0.1-0.2MPa, and the temperature of heating crystallization is 90-100 ℃.|[0055] Specific examples are as follows:|[0056] the electrolytic aluminum scraps used in the following examples were in the form of hard blocks, the carbon content was approximately half, and the main components of the materials are shown in Table 1. |[0057] TABLE 1 electrolytic aluminum scrap composition content|[0058] |[0059] Example 1|[0060] (1) Taking a certain amount of electrolytic aluminum scraps, and coarsely crushing the scraps into small blocks with the length of about 5 cm.|[0061] (2) Weighing 4000g of sieved material, placing the sieved material into a crucible, placing the crucible into a calciner, calcining at 700 ℃ for 5 hours, cooling to room temperature, taking out the material, and primarily crushing the material into small blocks with the size of 1-5 mm.|[0062] (3) Adding the decarbonized material into a mechanical strengthening leaching kettle, adding zirconia balls with the weight of 1:1 into the slurry liquid-solid ratio of 5:1, starting heating and stirring, heating to 80 ℃ for leaching, adding 98% sulfuric acid to adjust the pH value to 3.5, leaching for 2 hours, filtering after leaching, obtaining leaching liquid and leaching residues after filtering, washing the leaching residues twice, piling up the leaching residues, returning the leaching residues to the leaching, connecting the leaching kettle with an absorbing device, wherein the absorbing liquid is dilute alkali solution, absorbing HF gas generated in the leaching process, the lithium leaching rate is 99.39%, the iron leaching rate is 35.35%, and the aluminum leaching rate is only about 2.11%.|[0063] (4) And (3) removing impurities from the leaching solution by two sections, wherein one section is to add hydrogen peroxide with the theoretical amount of 1.2 times, then add 5% sodium hydroxide to adjust the pH value to 4.5, keep the reaction temperature to 60 ℃, react for 4 hours, filter the obtained filtrate and filter residues, slurry and wash the filter residues twice, perform two sections of impurity removal on the filtrate, add 2g of calcium remover oxalic acid, then add 5% sodium hydroxide to adjust the pH value to 12.5, react for 3 hours, filter the obtained lithium-containing filtrate and impurity filter residues, and store the filter residues.|[0064] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, cooling to 0 ℃ and carrying out one-stage freezing and crystallizing of sodium sulfate to obtain the liquid after denitration.|[0065] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at 90 ℃ to obtain crude lithium carbonate.|[0066] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.1MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0067] Example 2|[0068] (1) Taking a certain amount of electrolytic aluminum scraps, and coarsely crushing the scraps into small blocks with the length of about 5 cm.|[0069] (2) Weighing 1000g of the sieved material, placing the material into a crucible, placing the crucible into a calciner, calcining at 1000 ℃ for 3 hours, cooling to room temperature, taking out the material, and primarily crushing the material into small pieces with the size of 1-5 mm.|[0070] (3) Adding the decarbonized material into a mechanical strengthening leaching kettle, adding zirconia balls with the weight of 1:1.1 into the slurry liquid in a solid ratio of 5:1, starting heating and stirring, heating to 60 ℃ for leaching, adding 98% sulfuric acid to adjust the pH value to 3.0, leaching for 1h, filtering after leaching, obtaining leaching liquid and leaching slag after filtering, piling the leaching slag after twice washing, and returning the leaching slag washing water to leaching, wherein the lithium leaching rate is 99.52%, the iron leaching rate is 36.77%, and the aluminum leaching rate is only 2.02%.|[0071] (4) And (3) removing impurities from the leaching solution by two sections, wherein one section is to add sodium chlorate with the theoretical amount of 1.1 times to the leaching solution, then add 10% sodium hydroxide to adjust the pH value to 4.5, keep the reaction temperature to 70 ℃, the reaction time to 2 hours, filter the obtained filtrate and filter residues, slurrying and washing the filter residues twice, performing two sections of impurity removal on the filtrate, adding 1g of calcium remover oxalic acid, then adding 10% sodium hydroxide to adjust the pH value to 12.0, the reaction time to 5 hours, and filtering to obtain filtrate containing lithium and filter residues containing impurities, and piling the filter residues.|[0072] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, cooling to 10 ℃ and carrying out one-stage freezing and crystallizing of sodium sulfate to obtain the denitrated liquid.|[0073] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at the temperature of 95 ℃ to obtain crude lithium carbonate.|[0074] (7) Adding 9 times of pure water into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.2MPa, performing precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0075] Example 3|[0076] (1) Taking a certain amount of electrolytic aluminum scraps, and coarsely crushing the scraps into small blocks with the length of about 5 cm.|[0077] (2) Weighing 15000g of sieved material, placing the sieved material into a crucible, placing the crucible into a calciner, calcining at 1600 ℃ for 5 hours, cooling to room temperature, taking out the material, and primarily crushing the material into small pieces with the size of 1-5 mm.|[0078] (3) Adding the decarbonized material into a mechanical strengthening leaching kettle, adding zirconia balls with the weight of 1:1.5 into the slurry liquid in a solid ratio of 3:1, starting heating and stirring, heating to 90 ℃ for leaching, adding 98% sulfuric acid to adjust the pH value to 4.0, leaching for 3 hours, filtering after leaching, obtaining leaching liquid and leaching slag after filtering, piling the leaching slag after twice washing, and returning the leaching slag washing water to leaching, wherein the lithium leaching rate is 99.02%, the iron leaching rate is 36.52%, and the aluminum leaching rate is only 2.00%.|[0079] (4) And (3) removing impurities from the leaching solution by two sections, wherein one section is to introduce oxygen into the leaching solution to oxidize all ferrous iron in the lithium solution into ferric iron, then adding 20% sodium hydroxide to adjust the pH value to 4.5, keeping the reaction temperature to 65 ℃, reacting for 5 hours, filtering to obtain filtrate and filter residue, pulping and washing the filter residue twice, performing two sections of impurity removal on the filtrate, adding 10g of calcium remover oxalic acid, then adding 20% sodium hydroxide to adjust the pH value to 13.0, reacting for 2 hours, filtering to obtain lithium-containing filtrate and impurity filter residue, and piling the filter residue.|[0080] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, cooling to-10 ℃ and carrying out one-stage freezing and crystallizing of sodium sulfate to obtain the liquid after denitration.|[0081] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at 98 ℃ to obtain crude lithium carbonate.|[0082] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.2MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0083] Comparative example 1|[0084] (1) Taking a certain amount of electrolytic aluminum scraps, and coarsely crushing the scraps into small blocks with the length of about 5 cm.|[0085] (2) Weighing 4000g of sieved material, placing the sieved material into a crucible, placing the crucible into a calciner, calcining at 700 ℃ for 5 hours, cooling to room temperature, taking out the material, and primarily crushing the material into small blocks with the size of 1-5 mm.|[0086] (3) Adding the decarbonized material into a leaching kettle, adding the slurry liquid into the leaching kettle, heating and stirring the mixture, heating the mixture to 80 ℃ for leaching, adding 98% sulfuric acid to adjust the pH value to 3.5, leaching for 2 hours, filtering the leached product, obtaining leaching liquid and leaching residues after filtering, piling the leaching residues after washing twice, returning the leaching residue washing water to the leaching, connecting the leaching kettle with an absorption device, and absorbing the absorption liquid into dilute alkali liquid, wherein the absorption liquid is HF gas generated in the leaching process, the lithium leaching rate is 89.52%, the iron leaching rate is 34.12%, and the aluminum leaching rate is only 1.95%.|[0087] (4) Removing impurities, namely adding 5% sodium hydroxide to adjust the pH value to 12.5, keeping the reaction temperature to be 60 ℃, and filtering to obtain filtrate and filter residue, pulping and washing the filter residue twice, wherein the reaction time is 5 hours.|[0088] (5) Concentrating and denitrating, namely heating and concentrating filtrate, and freezing and crystallizing sodium sulfate for one time to obtain denitrated liquid.|[0089] (6) And precipitating lithium, namely adding sodium carbonate into the denitration liquid to obtain crude lithium carbonate by precipitation.|[0090] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.1MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the lithium carbonate.|[0091] Table 2 composition of final lithium carbonate product in examples and comparative examples|[0092] |[0093] While certain exemplary embodiments of the present application have been described above, it should be understood that they have been presented by way of example only, and not limitation, to the scope of the application. The features of these embodiments may be recombined in a suitable manner while still obtaining a solution that is within the scope of the application as claimed. Based on the above embodiments, all other embodiments obtained by those skilled in the art without making creative efforts, i.e., all modifications, equivalents, improvements etc., which are within the spirit and principles of the present application, fall within the protection scope of the present application as claimed. (CN119800102)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for extracting lithium from electrolytic aluminum waste by mechanical reinforcement and a mechanical reinforcement leaching kettle.|BACKGROUND ART|[0002] In recent years, the country has brought out a series of policies to the new energy and energy storage industry to encourage development, and a plurality of leading enterprises such as Ningde times, BI, guo Xuan Gao and the like in the industry lead the new energy industry of China to go forward in the world, and the development of the new energy industry simultaneously drives the layout of lithium resources and the development and continuous progress of lithium extraction technology.|[0003] The electrolytic aluminum industry forms an aluminum production system in China aluminum industry, guangxi apple aluminum industry, south flat aluminum industry and the like, the quantity and the scale of enterprises are continuously increased along with the economic development, the yield of electrolytic aluminum waste residues is continuously increased, the electrolytic aluminum waste residues contain a certain amount of lithium and cryolite, and due to the rising of the price of the lithium, a great deal of research is developed on the extraction and utilization technology of the lithium in the aluminum waste residues in recent years, and enterprises such as polyfluoro, xinjiang weapon groups and the like have industrialized layout, so that the lithium and aluminum resources can be greatly saved.|[0004] For example, china patent with the application number 2022113448491 discloses a method and equipment for recycling electrolytic aluminum waste residues, wherein the electrolytic aluminum waste residues are pulped with sulfuric acid for sulfating roasting, the roasted materials are hydrolyzed, alkali is added into the filtered solution for producing aluminum hydroxide precipitation, sodium carbonate is added into the filtrate for forming sodium sulfate, and the recycled hydrogen fluoride, aluminum hydroxide and sodium sulfate synthetic cryolite are sold to an electrolytic aluminum factory.|[0005] The Chinese patent with the application number 2023107040418 discloses a process method for improving the lithium leaching rate in refractory aluminum electrolysis waste residues, which comprises the following steps of preparing 10L of 5% aluminum trichloride solution, adding 10g of waste residues into every 100ml of aluminum trichloride solution, adding 1kg of waste residues together, controlling the final pH value to be 3, leaching at room temperature for 2 hours, filtering and washing the filter residues, wherein the filter residues mainly contain impurities such as carbon, and the filtrate enters a impurity removal enrichment purification process. According to the invention, the lithium sodium cryolite in the refractory electrolytic aluminum waste residue is dissolved by adopting the aluminum salt solution, so that lithium in the refractory electrolytic aluminum waste residue can be converted into lithium chloride or lithium sulfate, the lithium leaching rate in the refractory electrolytic aluminum waste residue is improved, and the problems of lower lithium leaching rate and environmental friendliness in the existing recovery process are effectively solved. According to the method, aluminum trichloride is used as a dissolution medium, the leaching solution contains extremely high aluminum content, and the recovery of lithium is affected although the leaching rate of lithium is relatively high.|[0006] In addition, aiming at the electrolytic aluminum waste residue with very high sodium and aluminum contents and nearly half of carbon, the amount of sulfuric acid and sodium hydroxide required for extracting all aluminum and lithium in the electrolytic aluminum waste residue is very large, the crystallization amount of sodium sulfate is large, the existence of carbon can cause large precipitation slag amount, the precipitation filtration property is poor, and the total recovery rate of lithium is affected. Therefore, there is a need to develop a simpler, economical and efficient method for extracting lithium from electrolytic aluminum slag to solve the above problems.|DISCLOSURE|Disclosure of Invention|[0007] Therefore, in order to solve the problems existing in the prior art, the invention provides a method for mechanically strengthening and extracting lithium from electrolytic aluminum waste and a mechanically strengthening leaching kettle, wherein the method selectively extracts lithium from waste aluminum slag by controlling leaching conditions, limits leaching of impurities such as aluminum, iron and the like in the slag, and further prepares lithium carbonate from lithium sulfate, and specifically comprises the following steps:|[0008] step 1, crushing electrolytic aluminum waste with carbon content more than 45% and aluminum content more than 10 times of lithium content; |[0009] Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and coarsely grinding to a granularity of 1-5mm to obtain a carbon-removed material; |[0010] Step 3, carrying out mechanical strengthening acid leaching on the carbon-removed material, namely carrying out fine grinding and selective leaching on the carbon-removed material in a mechanical strengthening leaching kettle, and filtering to obtain leaching liquid and leaching slag; |[0011] Step 4, performing two-stage impurity removal, wherein the first stage impurity removal process comprises the steps of adding an oxidant into the leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues; |[0012] Step 5, heating and concentrating the filtrate containing lithium, and then freezing and crystallizing to obtain a denitration liquid; |[0013] Step 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate; |[0014] And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. |[0015] Further, the electrolytic aluminum scraps in the step 1 comprise, by mass, 1% -1.1% of lithium, 12.2% -13.0% of aluminum, 11.0% -12.0% of sodium, 0.8% -0.9% of iron, 1.5% -2.0% of calcium, 0.24% -0.26% of magnesium, 0.1% of silicon, 13.0% -13.5% of fluorine, 0.14% -0.15% of sulfur, 0.1% of manganese, 45% of carbon and the balance of water.|[0016] Further, the size of the crushed electrolytic aluminum scraps in the step 1 is 1-10cm.|[0017] Further, in the step 3, the slurry liquid-solid ratio of water to the carbon removal material in the leaching process is 3-5:1, the mass ratio of the carbon removal material to the grinding balls is 1:1-1.5, the leaching agent is 98% sulfuric acid, the leaching temperature is 60-90 ℃, and the leaching time is 1-3 hours.|[0018] Further, the oxidant in the first stage of impurity removal in the step 4 is hydrogen peroxide, sodium chlorate, sodium hypochlorite, chlorine, air and oxygen, the impurity removal temperature is 55-70 ℃, alkali is sodium hydroxide solution with the mass concentration of 5-20%, the reaction time is 1-5h, the reaction time in the second stage of impurity removal is 1-5h, the calcium remover is oxalic acid, and the amount of the added calcium remover is 0.05% -0.1% of the electrolytic aluminum waste.|[0019] Further, the temperature of the freeze crystallization in the step 5 is-10 ℃ to 10 ℃.|[0020] Further, the heating temperature in step 6 is 90-100 ℃.|[0021] Further, in the step 7, the mass ratio of the pure water to the crude lithium carbonate is 9-10:1, and the pressure of the CO 2 gas is 0.1-0.2MPa.|[0022] Further, the temperature of the heating crystallization in the step 7 is 90-100 ℃.|[0023] The mechanical strengthening leaching kettle used in the step 3 comprises a kettle body, a jacket, a tank cover, a liquid adding port, a stirring device and grinding balls, wherein the jacket is coated on the outer side of the kettle body, a heating pipe is arranged in the jacket, the tank cover is positioned above the kettle body, the liquid adding port is arranged on the tank cover, the stirring device comprises a motor, a speed reducer, a stirring shaft and a stirring paddle on the outer side of the stirring shaft, the motor and the speed reducer are positioned on the tank cover, the stirring shaft is connected with the motor and the speed reducer, the stirring shaft and the stirring paddle are positioned in the kettle body, the grinding balls are arranged in the kettle body, and the grinding balls are zirconia balls.|[0024] Compared with the prior art, the invention has the following advantages:|[0025] (1) The electrolytic aluminum waste material is first calcined or burnt to eliminate most of carbon, and this can raise the lithium extracting capacity by almost one time, the concentration of lithium solution by about one time, lower the treating difficulty and cost and raise the lithium recovering rate and treating efficiency. |[0026] (2) According to the invention, by controlling the pH value in the leaching process to be 3.0-4.0, lithium in the electrolytic aluminum waste is dissolved out, most of aluminum, iron, sodium, fluorine and the like are not dissolved out and remain in leaching residues, so that the use amount of leaching acid is reduced, the use amount of impurity-removing alkali is greatly reduced, the residue filtering performance is good, the sodium content in the lithium solution after impurity removal is greatly reduced, the requirement can be met only by one-time denitration, the burden of each process is reduced, and the lithium extraction cost and the operation difficulty are reduced. Because the aluminum content in the material is very high, the lithium solution after impurity removal is relatively high in sodium content, and the leaching of aluminum is inhibited by controlling the acidity of the leaching solution, so that the loss of lithium caused by the fact that aluminum hydroxide is colloid during alkali addition and impurity removal is reduced.|[0027] (3) The invention adopts a mechanical strengthening method to strengthen leaching, solves the problems of high hardness and difficult fine grinding of the material, adopts a mechanical strengthening method to grind and leach simultaneously, increases the surface activity of the material and increases the active point of the material, thereby improving the treatment efficiency of electrolytic aluminum waste and the extraction rate of lithium, and the leaching rate of lithium can reach more than 95 percent, and has mild leaching condition and high treatment efficiency. The carbon in the leaching slag can be used as fuel, and most of the leaching slag is cryolite which can be used later.|[0028] (4) The lithium leaching solution is subjected to two-stage impurity removal, wherein the first stage impurity removal is performed to remove aluminum impurities, the second stage impurity removal is performed to remove other impurities such as iron, manganese, calcium and the like, and the two-stage impurity removal main products are different and are treated respectively. In the second-stage impurity removal process, oxalic acid is used as a calcium remover instead of conventional ion exchange resin, so that excessive waste water is avoided, the problem that the ion exchange resin is easy to scale in a sulfuric acid system is avoided, and the calcium remover can remove calcium efficiently and the system operates smoothly.|[0029] The method can effectively extract lithium in the electrolytic aluminum waste to prepare battery grade lithium carbonate, and the leaching slag mainly comprises cryolite, so that the method can be used and has good economic benefit.|DRAWINGS DESCRIPTION|[0030] Embodiments of the invention are further described below with reference to the accompanying drawings, in which:|[0031] FIG. 1 shows a process flow diagram of the present invention; |[0032] fig. 2 shows a cross-sectional view and a top view of the structure of the apparatus of the mechanically reinforced leaching tank. |[0033] The device comprises a 1-motor, a 2-speed reducer, a 3-tank cover, a 4-kettle body, a 5-stirring shaft, a 6-stirring paddle, a 7-jacket, an 8-grinding ball, a 9-heating pipe, a 10-valve, an 11-liquid adding port, a 12-hinge and 13-slurry.|INVENTION MODE|Detailed Description|[0034] In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail by the following examples with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0035] The mechanical strengthening leaching kettle comprises a kettle body 4, a jacket 7, a tank cover 3, a liquid adding opening 11, a stirring device and grinding balls 8, wherein the jacket 7 is coated on the outer side of the kettle body 4 and is internally provided with a heating pipe 9, the tank cover 3 is positioned above the kettle body 4, the tank cover 3 is provided with two liquid adding openings 11, the stirring device comprises a motor 1, a speed reducer 2, a stirring shaft 5 and stirring paddles 6 on the outer side of the stirring shaft, the motor 1 and the speed reducer 2 are positioned on the tank cover 3, the stirring shaft 5 is connected with the motor 1 and the speed reducer 2, the stirring shaft 5 and the stirring paddles 6 are positioned in the kettle body 4, a plurality of grinding balls 8 are arranged in the kettle body 4, and the grinding balls 8 are zirconia balls and are mixed with slurry 13. The outlet pipeline below the kettle body 4 is also provided with a valve 10, and when the slag amount of the system is small, filter cloth can be arranged on the lower pipeline for filtering. The tank cover 3 is a half-open tank cover and is divided into two parts, and the two parts are connected through a hinge 12 so as to realize half-open, so that the grinding balls can be conveniently placed and taken out.|[0036] A method for preparing battery grade lithium carbonate by electrolyzing aluminum scraps, which comprises the following steps:|[0037] the method comprises the steps of 1, crushing or manually crushing electrolytic aluminum waste with carbon content more than 45% and aluminum content more than 10 times of lithium content by a crusher, wherein the size of the crushed electrolytic aluminum waste is 1-10cm, the components and mass ratio of the electrolytic aluminum waste are respectively 1% -1.1% of lithium, 12.2-13.0% of aluminum, 11.0-12.0% of sodium, 0.8-0.9% of iron, 1.5-2.0% of calcium, 0.24-0.26% of magnesium, <0.1% of silicon, 13.0-13.5% of fluorine, 0.14-0.15% of sulfur, <0.1% of manganese, 45% of carbon and the balance of water. |[0038] Step 2, calcining the crushed electrolytic aluminum waste at a high temperature of 550-1600 ℃ for 0.5-5 hours to remove carbon therein, and then cooling and coarsely grinding to a granularity of 1-5mm to obtain a carbon-removed material;|[0039] and 3, carrying out mechanical strengthening acid leaching on the carbon-removed material, namely carrying out fine grinding and selective leaching on the carbon-removed material in a mechanical strengthening leaching kettle, regulating the leaching pH value to 3.0-4.0, filtering to obtain leaching liquid and leaching slag, washing the leaching slag twice, piling up the leaching slag after filtering, and returning the leaching slag washing water to leaching, wherein the slurry liquid-solid ratio of the carbon-removed material to water in the leaching process is 3-5:1, the mass ratio of the carbon-removed material to the grinding balls is 1:1-1.5, the leaching agent is 98% sulfuric acid, the leaching temperature is 60-90 ℃, and the leaching time is 1-3h. The leaching kettle is connected with an absorption device, and absorption liquid in the absorption device is dilute alkali liquid and absorbs fluorine and acid mist generated in the leaching process. |[0040] 2LiF+H2SO4→Li2SO4+2HF↑|[0041] 2Na3AlF6+6H2SO4→3Na2SO4+Al2(SO4)3+6HF↑|[0042] Fe+H2SO4→FeSO4+H2↑|[0043] Step 4, performing two-stage impurity removal, wherein the one-stage impurity removal process comprises the steps of adding an oxidant into the one-stage leaching solution, adding alkali to adjust the pH value to be 4.5-5.0, and filtering to obtain filtrate and filter residues, wherein the oxidant in the one-stage impurity removal process is hydrogen peroxide, sodium chlorate, sodium hypochlorite, chlorine, air and oxygen, the impurity removal temperature is 55-70 ℃, the alkali is sodium hydroxide solution with the mass concentration of 5-20%, and the reaction time is 1-5h;|[0044] 2FeSO4+H2SO4+H2O2→Fe2(SO4)3+2H2O( Chemical equation using hydrogen peroxide as oxidant |[0045] Al2(SO4)3+6NaOH→3Na2SO4+2Al(OH)3↓|[0046] Fe2(SO4)3+6NaOH→3Na2SO4+2Fe(OH)3↓|[0047] The second stage of impurity removing process is that adding calcium removing agent into filtrate, adding alkali to regulate pH value to 12.0-13.0, filtering to obtain lithium-containing filtrate and impurity filtering residue, and the reaction time in the second stage of impurity removing process is 1-5h, and the added calcium removing agent is 0.05% -0.1% of the electrolytic aluminum waste material.|[0048] Mn2++2NaOH→2Na++Mn(OH)2↓|[0049] H2C2O4+Ca2+→CaC2O4↓+2H+|[0050] Mg2++2NaOH→2Na++Mg(OH)2↓|[0051] And 5, heating and concentrating the filtrate containing lithium, and performing one-stage freezing crystallization to obtain a liquid after denitration, wherein the temperature of the freezing crystallization is between-10 ℃ and 10 ℃, and removing sodium sulfate.|[0052] And 6, adding sodium carbonate solution into the denitration liquid under the heating condition, precipitating and filtering to obtain crude lithium carbonate, wherein the heating temperature is 90-100 ℃.|[0053] Li2SO4+Na2CO3→Li2CO3↓+2Na2SO4|[0054] And 7, dissolving the crude sodium carbonate by using pure water, introducing CO 2 gas into the solution, precisely filtering to obtain a lithium carbonate solution after the crude sodium carbonate is completely dissolved, and heating for crystallization, filtering, washing and drying to obtain the battery grade lithium carbonate. The mass ratio of the pure water to the crude lithium carbonate is 9-10:1, the pressure of the CO 2 gas is 0.1-0.2MPa, and the temperature of heating crystallization is 90-100 ℃.|[0055] Specific examples are as follows:|[0056] the electrolytic aluminum scraps used in the following examples were in the form of hard blocks, the carbon content was approximately half, and the main components of the materials are shown in Table 1. |[0057] TABLE 1 electrolytic aluminum scrap composition content|[0058] |[0059] Example 1|[0060] (1) Taking a certain amount of electrolytic aluminum scraps, and coarsely crushing the scraps into small blocks with the length of about 5 cm.|[0061] (2) Weighing 4000g of sieved material, placing the sieved material into a crucible, placing the crucible into a calciner, calcining at 700 ℃ for 5 hours, cooling to room temperature, taking out the material, and primarily crushing the material into small blocks with the size of 1-5 mm.|[0062] (3) Adding the decarbonized material into a mechanical strengthening leaching kettle, adding zirconia balls with the weight of 1:1 into the slurry liquid-solid ratio of 5:1, starting heating and stirring, heating to 80 ℃ for leaching, adding 98% sulfuric acid to adjust the pH value to 3.5, leaching for 2 hours, filtering after leaching, obtaining leaching liquid and leaching residues after filtering, washing the leaching residues twice, piling up the leaching residues, returning the leaching residues to the leaching, connecting the leaching kettle with an absorbing device, wherein the absorbing liquid is dilute alkali solution, absorbing HF gas generated in the leaching process, the lithium leaching rate is 99.39%, the iron leaching rate is 35.35%, and the aluminum leaching rate is only about 2.11%.|[0063] (4) And (3) removing impurities from the leaching solution by two sections, wherein one section is to add hydrogen peroxide with the theoretical amount of 1.2 times, then add 5% sodium hydroxide to adjust the pH value to 4.5, keep the reaction temperature to 60 ℃, react for 4 hours, filter the obtained filtrate and filter residues, slurry and wash the filter residues twice, perform two sections of impurity removal on the filtrate, add 2g of calcium remover oxalic acid, then add 5% sodium hydroxide to adjust the pH value to 12.5, react for 3 hours, filter the obtained lithium-containing filtrate and impurity filter residues, and store the filter residues.|[0064] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, cooling to 0 ℃ and carrying out one-stage freezing and crystallizing of sodium sulfate to obtain the liquid after denitration.|[0065] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at 90 ℃ to obtain crude lithium carbonate.|[0066] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.1MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0067] Example 2|[0068] (1) Taking a certain amount of electrolytic aluminum scraps, and coarsely crushing the scraps into small blocks with the length of about 5 cm.|[0069] (2) Weighing 1000g of the sieved material, placing the material into a crucible, placing the crucible into a calciner, calcining at 1000 ℃ for 3 hours, cooling to room temperature, taking out the material, and primarily crushing the material into small pieces with the size of 1-5 mm.|[0070] (3) Adding the decarbonized material into a mechanical strengthening leaching kettle, adding zirconia balls with the weight of 1:1.1 into the slurry liquid in a solid ratio of 5:1, starting heating and stirring, heating to 60 ℃ for leaching, adding 98% sulfuric acid to adjust the pH value to 3.0, leaching for 1h, filtering after leaching, obtaining leaching liquid and leaching slag after filtering, piling the leaching slag after twice washing, and returning the leaching slag washing water to leaching, wherein the lithium leaching rate is 99.52%, the iron leaching rate is 36.77%, and the aluminum leaching rate is only 2.02%.|[0071] (4) And (3) removing impurities from the leaching solution by two sections, wherein one section is to add sodium chlorate with the theoretical amount of 1.1 times to the leaching solution, then add 10% sodium hydroxide to adjust the pH value to 4.5, keep the reaction temperature to 70 ℃, the reaction time to 2 hours, filter the obtained filtrate and filter residues, slurrying and washing the filter residues twice, performing two sections of impurity removal on the filtrate, adding 1g of calcium remover oxalic acid, then adding 10% sodium hydroxide to adjust the pH value to 12.0, the reaction time to 5 hours, and filtering to obtain filtrate containing lithium and filter residues containing impurities, and piling the filter residues.|[0072] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, cooling to 10 ℃ and carrying out one-stage freezing and crystallizing of sodium sulfate to obtain the denitrated liquid.|[0073] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at the temperature of 95 ℃ to obtain crude lithium carbonate.|[0074] (7) Adding 9 times of pure water into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.2MPa, performing precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0075] Example 3|[0076] (1) Taking a certain amount of electrolytic aluminum scraps, and coarsely crushing the scraps into small blocks with the length of about 5 cm.|[0077] (2) Weighing 15000g of sieved material, placing the sieved material into a crucible, placing the crucible into a calciner, calcining at 1600 ℃ for 5 hours, cooling to room temperature, taking out the material, and primarily crushing the material into small pieces with the size of 1-5 mm.|[0078] (3) Adding the decarbonized material into a mechanical strengthening leaching kettle, adding zirconia balls with the weight of 1:1.5 into the slurry liquid in a solid ratio of 3:1, starting heating and stirring, heating to 90 ℃ for leaching, adding 98% sulfuric acid to adjust the pH value to 4.0, leaching for 3 hours, filtering after leaching, obtaining leaching liquid and leaching slag after filtering, piling the leaching slag after twice washing, and returning the leaching slag washing water to leaching, wherein the lithium leaching rate is 99.02%, the iron leaching rate is 36.52%, and the aluminum leaching rate is only 2.00%.|[0079] (4) And (3) removing impurities from the leaching solution by two sections, wherein one section is to introduce oxygen into the leaching solution to oxidize all ferrous iron in the lithium solution into ferric iron, then adding 20% sodium hydroxide to adjust the pH value to 4.5, keeping the reaction temperature to 65 ℃, reacting for 5 hours, filtering to obtain filtrate and filter residue, pulping and washing the filter residue twice, performing two sections of impurity removal on the filtrate, adding 10g of calcium remover oxalic acid, then adding 20% sodium hydroxide to adjust the pH value to 13.0, reacting for 2 hours, filtering to obtain lithium-containing filtrate and impurity filter residue, and piling the filter residue.|[0080] (5) Concentrating and denitrating the filtrate containing lithium, heating and concentrating, cooling to-10 ℃ and carrying out one-stage freezing and crystallizing of sodium sulfate to obtain the liquid after denitration.|[0081] (6) And precipitating lithium by adding sodium carbonate into the denitration liquid at 98 ℃ to obtain crude lithium carbonate.|[0082] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.2MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the battery-grade lithium carbonate.|[0083] Comparative example 1|[0084] (1) Taking a certain amount of electrolytic aluminum scraps, and coarsely crushing the scraps into small blocks with the length of about 5 cm.|[0085] (2) Weighing 4000g of sieved material, placing the sieved material into a crucible, placing the crucible into a calciner, calcining at 700 ℃ for 5 hours, cooling to room temperature, taking out the material, and primarily crushing the material into small blocks with the size of 1-5 mm.|[0086] (3) Adding the decarbonized material into a leaching kettle, adding the slurry liquid into the leaching kettle, heating and stirring the mixture, heating the mixture to 80 ℃ for leaching, adding 98% sulfuric acid to adjust the pH value to 3.5, leaching for 2 hours, filtering the leached product, obtaining leaching liquid and leaching residues after filtering, piling the leaching residues after washing twice, returning the leaching residue washing water to the leaching, connecting the leaching kettle with an absorption device, and absorbing the absorption liquid into dilute alkali liquid, wherein the absorption liquid is HF gas generated in the leaching process, the lithium leaching rate is 89.52%, the iron leaching rate is 34.12%, and the aluminum leaching rate is only 1.95%.|[0087] (4) Removing impurities, namely adding 5% sodium hydroxide to adjust the pH value to 12.5, keeping the reaction temperature to be 60 ℃, and filtering to obtain filtrate and filter residue, pulping and washing the filter residue twice, wherein the reaction time is 5 hours.|[0088] (5) Concentrating and denitrating, namely heating and concentrating filtrate, and freezing and crystallizing sodium sulfate for one time to obtain denitrated liquid.|[0089] (6) And precipitating lithium, namely adding sodium carbonate into the denitration liquid to obtain crude lithium carbonate by precipitation.|[0090] (7) Adding pure water with the mass of 10 times into the crude lithium carbonate for dissolution, then introducing CO 2 gas, introducing CO 2 gas with the pressure of 0.1MPa, carrying out precise filtration after the lithium carbonate is completely dissolved to obtain a lithium carbonate solution, heating the lithium solution to a boiling point (90-100 ℃) for crystallization, filtering, washing and drying to obtain the lithium carbonate.|[0091] Table 2 composition of final lithium carbonate product in examples and comparative examples|[0092] |[0093] While certain exemplary embodiments of the present application have been described above, it should be understood that they have been presented by way of example only, and not limitation, to the scope of the application. The features of these embodiments may be recombined in a suitable manner while still obtaining a solution that is within the scope of the application as claimed. Based on the above embodiments, all other embodiments obtained by those skilled in the art without making creative efforts, i.e., all modifications, equivalents, improvements etc., which are within the spirit and principles of the present application, fall within the protection scope of the present application as claimed. Family Number|(114163661)|114163661|Abstract|(CN119800102 A)|The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium - containing waste , in particular to a method for extracting lithium from electrolytic aluminum waste through mechanical strengthening and a mechanical strengthening leaching kettle . The method comprises the following steps : ( 1 ) coarsely crushing the electrolytic aluminum waste ; ( 2 ) calcining or combusting the electrolytic aluminum waste to remove carbon ; ( 3 ) after carbon removal , the electrolytic aluminum waste is subjected to mechanical strengthening , and lithium is selectively leached by controlling the leaching acidity ; ( 4 ) performing two - stage impurity removal on the lithium leachate ; and ( 5 ) concentrating and denitrifying the impurity - removed liquid , precipitating lithium , carbonizing and crystallizing to prepare the battery - grade lithium carbonate . According to the method , carbon in the electrolytic aluminum waste is removed through a calcination or combustion method , leaching of lithium is strengthened through a mechanical strengthening method , meanwhile , the leaching condition is controlled to enable lithium in the waste aluminum slag to be dissolved out into a leaching solution , and aluminum , iron , sodium and most fluorine in the waste aluminum slag are not dissolved out and left in the leaching slag . And performing simple impurity removal , concentration and denitration on the leachate to prepare the battery - grade lithium carbonate . The method is simple in process and high in lithium extraction rate , and cryolite is mainly contained in leaching residues and can be utilized subsequently . |IPC codes|(CN119800102 A)|C01D - 015/08 | Materials, metallurgy Y02P-010/20 Y02P-010/20 C01D-015/08|C22B-001/00|C22B-003/02|C22B-007/00|C22B-026/12 C01D-015/08|C22B-001/00|C22B-003/02|C22B-007/00|C22B-026/12 PENDING (CN119800102)|PENDING ALIVE (CN119800102)|ALIVE (CN119800102)|LEGAL DETAILS FOR CN119800102|Actual or expected expiration date=2044-12-02|Legal state=ALIVE|Status=PENDING|Event publication date=2024-12-02|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202411750435|Application date=2024-12-02|Standardized application number=2024CN-1750435|Event publication date=2025-04-11|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN119800102|Publication stage code=A|Publication date=2025-04-11|Standardized publication number=CN119800102|Event publication date=2025-04-11|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-04-29|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN119800102)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQUsOI7QR9sqFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000077162915&ekey=2332&xpn=CN119800102&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=qZH5iJ5PU3rbhnGM9QX%252BXZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN119800102)|CN (CN119800102)|NAME=JINCHUAN GROUP CO. LTD. , COUNTRY=CN (CN119800102)|NAME=LI ZIJIAN;CHINA NONFERROUS METALS INDUSTRY PATENT CENTER , REG=11028 (CN119800102)|NAME=CHAI GENFENG|NAME=BAI YANLI|NAME=YANG XIAOYAN|NAME=WANG JUANHUI|NAME=CHEN TIANYI|NAME=WANG QIAN|NAME=SONG FANG|NAME=YAN XIANYONG 0 1 Titre: (CN119800102)|Method for extracting lithium from electrolytic aluminum waste through mechanical strengthening and mechanical strengthening leaching kettle Résumé: (CN119800102)|The invention relates to the technical field of extraction and utilization of electrolytic aluminum lithium-containing waste, in particular to a method for extracting lithium from electrolytic aluminum waste through mechanical strengthening and a mechanical strengthening leaching kettle. The method comprises the following steps: (1) coarsely crushing the electrolytic aluminum waste; (2) calcining or combusting the electrolytic aluminum waste to remove carbon; (3) after carbon removal, the electrolytic aluminum waste is subjected to mechanical strengthening, and lithium is selectively leached by controlling the leaching acidity; (4) performing two-stage impurity removal on the lithium leachate; and (5) concentrating and denitrifying the impurity-removed liquid, precipitating lithium, carbonizing and crystallizing to prepare the battery-grade lithium carbonate. According to the method, carbon in the electrolytic aluminum waste is removed through a calcination or combustion method, leaching of lithium is strengthened through a mechanical strengthening method, meanwhile, the leaching condition is controlled to enable lithium in the waste aluminum slag to be dissolved out into a leaching solution, and aluminum, iron, sodium and most fluorine in the waste aluminum slag are not dissolved out and left in the leaching slag. And performing simple impurity removal, concentration and denitration on the leachate to prepare the battery-grade lithium carbonate. The method is simple in process and high in lithium extraction rate, and cryolite is mainly contained in leaching residues and can be utilized subsequently. 100 Abstract gpt-4o-mini no The article focuses on lithium extraction from electrolytic aluminum waste and does not address accelerated weathering or CO₂ capture.
106 CN201210039920 CN201210039920 CN102580674|CN102580674 7775753 CN102580674 B 2013-08-14 [CN102580674B]|CN102580674 A 2012-07-18 [CN102580674] 2012-02-21 2012-02-21 2013-08-14|2012-07-18 (CN102580674B)|2013-08-14 (CN102580674)|2014-02-21 (CN102580674)|Method for preparing mercury removal agent by utilizing modified waste tire pyrolysis residue (CN102580674)|The invention discloses a method for preparing a mercury removal agent by utilizing a modified waste tire pyrolysis residue. The method comprises the following steps: (1) crushing the waste tire pyrolysis residue, wherein the particle sizes of particles are 60-200 meshes; (2) immersing hydrochloric acid or sulfuric acid water solution with the concentration of 30-60wt% into the waste tire pyrolysis residue in an isovolumetric manner, continuously stirring for 1h at room temperature, then drying for 48h at a temperature of 110 DEG C; and (3) activating the pyrolysis residue subjected to the acid immersion in a sealed furnace body in the atmosphere of nitrogen by using high-temperature vapor at a temperature of 800-1000 DEG C for 1-3h so as to obtain the mercury removal agent. The method has the advantages that: the mercury removal agent prepared by the modified pyrolysis residue enables the pyrolysis residue to become profitable, the price of the modified pyrolysis residue is lower than that of the modified active carbon, high mercury removal rate can be achieved at the same time, and the adsorption capacity of the modified pyrolysis residue for mercury is up to 800 mug/g. UNIVERSITY OF NANKAI (CN102580674)|NANKAI UNIVERSITY|(CN102580674)|NANKAI UNIVERSITY SHEN BOXIONG (CN102580674)|SHEN BOXIONG|(CN102580674)|SHEN BOXIONG (CN102580674)|HOU LI;TIANJIN JIAMENG INTETTECTUAL PROPERTY AGENT CO. LTD. (CN102580674)|The invention aims to provide a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis residues, aiming at the technical analysis, the mercury removing agent prepared by the method changes the pyrolysis residues into valuables, has the advantage of higher price than modified activated carbon, can obtain higher mercury removing rate, and the adsorption capacity of the modified pyrolysis residues to mercury reaches 800 ug/g.|The invention has the advantages that: the prepared mercury removing agent for the modified pyrolysis slag changes the pyrolysis slag into valuable, has the advantage of higher price than modified activated carbon, and can obtain very high mercury removal rate, and the mercury adsorption capacity of the modified pyrolysis slag reaches 800 ug/g.|These substances are advantageous for improving the chemisorption of mercury.|The pyrolytic slag accounts for about 35 percent of the waste tires and belongs to solid slag which is difficult to utilize.| (CN102580674)|1. A method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag is characterized by comprising the following steps: the method comprises the following operation steps:1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;2) soaking 30-60 wt% hydrochloric acid or sulfuric acid aqueous solution into the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying at 110 ℃ for 48 hours;3) and (3) activating the acid-impregnated pyrolysis residue by using high-temperature water vapor in a sealed furnace body under the nitrogen atmosphere, wherein the activation temperature is 800-1000 ℃, and the activation time is 1-3 hours, so that the mercury removing agent can be prepared.| (CN102580674)|In conclusion, the invention provides a method for modifying pyrolysis slag, which is a method for acid impregnation by an isometric method and then activation under high-temperature water vapor.|The invention provides a method for adsorbing mercury in flue gas by modifying waste tires.|The invention relates to a flue gas demercuration technology, in particular to a method for preparing a demercuration agent by utilizing modified waste tire pyrolysis residues.| (CN102580674)|MERCURY(100,37)|WASTE TIRE PYROLYSIS RESIDUE(100,11)|WASTE TIRE PYROLYSIS SLAG(100,9)|MODIFYING PYROLYSIS SLAG(68,1)|PYROLYTIC SLAG ACCOUNT(67,1)|MODIFIED PYROLYSIS SLAG(62,2)|MERCURY CHEMISORPTION(59,1)|PYROLYSIS RESIDUE(54,9)|ADSORBING MERCURY(48,1)|MERCURY ADSORPTION(43,7)|PYROLYSIS MODIFICATION(41,2)|MODIFIED PYROLYSIS RESIDUE(40,1)|ACID IMPREGNATED PYROLYSIS RESIDUE(38,7)|FLUE GAS DEMERCURATION(38,1)|PREPARED MERCURY(37,2)|DEBACTEROL AQUEOUS SOLUTION(36,5)|SEALED FURNACE(35,7)|MODIFYING WASTE TIRE(34,1)|ACID IMPREGNATION(32,1)|DEMERCURATION(32,1)|NITROGEN ATMOSPHERE(30,7)|PYROLYSIS(28,3)|MERCURY REMOVAL RATE(26,2)|SOLID SLAG(24,1)|ADSORPTION CAPACITY(23,10)|MODIFIED WASTE TIRE PYROLYSIS(22,6)|ACTIVATION TEMPERATURE(19,7)|ACTIVATED CARBON MODIFICATION(19,4)|AQUEOUS SOLUTION(18,7)|HYDROGEN CHLORIDE(14,8)|MERCURY OXIDE(12,5)|WASTE TIRE(12,5)|FLUE GAS(10,10)|PYROLYSIS SLAG(10,2)|ELEMENTAL MERCURY(9,10)|TECHNICAL ANALYSIS(9,2)|ACTIVATION TIME(8,7)|UG G(8,3)|SUBSTANCE MERCURY(8,2)|ACCELERATE CHEMISORPTION(8,1)|MERCURY ARTIFICIAL EMISSION(8,1)|PARTICLE SIZE(7,7)|ROOM TEMPERATURE(7,7)|HIGH COST(7,4)|RECLAIMED RUBBER(7,2)|TIRE RETREADING(7,1)|WET DESULPHURIZATION(7,1)|COAL BURNING(6,1)|DESORPTION PHENOMENON(6,1)|FOREIGN COUNTRY(6,1)|GRADUALLY PAID ATTENTION(6,1)|GRANULAR MERCURY(6,1)|LITERATURE REPORT(6,1)|MERCURY PARTICLE(6,1)|SCRAP TIRE THERMAL DECOMPOSITION(5,2)|COAL COMBUSTION FLUE GAS(5,1)|SUBSTANCE ADSORPTION(5,1)|DEBACTEROL(4,2)|METHANE(4,2)|ACID DIPPING(4,1)|ACID SOAK(4,1)|BROMINE LOADING(4,1)|GASEOUS SUBSTANCE(4,1)|INORGANIC MATTER(4,1)|INORGANIC SALT(4,1)|ISOVOLUMETRIC HYDROGEN CHLORIDE(4,1)|MERCURY DISCHARGE(4,1)|MNCL2THE FORMATION(4,1)|NONNEGLIGIBLE ENVIRONMENTAL FACTOR(4,1)||(CN102580674)|MERCURY(100,37)|WASTE TIRE PYROLYSIS RESIDUE(100,11)|WASTE TIRE PYROLYSIS SLAG(100,9)|MODIFYING PYROLYSIS SLAG(68,1)|PYROLYTIC SLAG ACCOUNT(67,1)|MODIFIED PYROLYSIS SLAG(62,2)|MERCURY CHEMISORPTION(59,1)|PYROLYSIS RESIDUE(54,9)|ADSORBING MERCURY(48,1)|MERCURY ADSORPTION(43,7)|PYROLYSIS MODIFICATION(41,2)|MODIFIED PYROLYSIS RESIDUE(40,1)|ACID IMPREGNATED PYROLYSIS RESIDUE(38,7)|FLUE GAS DEMERCURATION(38,1)|PREPARED MERCURY(37,2)|DEBACTEROL AQUEOUS SOLUTION(36,5)|SEALED FURNACE(35,7)|MODIFYING WASTE TIRE(34,1)|ACID IMPREGNATION(32,1)|DEMERCURATION(32,1)|NITROGEN ATMOSPHERE(30,7)|PYROLYSIS(28,3)|MERCURY REMOVAL RATE(26,2)|SOLID SLAG(24,1)|ADSORPTION CAPACITY(23,10)|MODIFIED WASTE TIRE PYROLYSIS(22,6)|ACTIVATION TEMPERATURE(19,7)|ACTIVATED CARBON MODIFICATION(19,4)|AQUEOUS SOLUTION(18,7)|HYDROGEN CHLORIDE(14,8)|MERCURY OXIDE(12,5)|WASTE TIRE(12,5)|FLUE GAS(10,10)|PYROLYSIS SLAG(10,2)|ELEMENTAL MERCURY(9,10)|TECHNICAL ANALYSIS(9,2)|ACTIVATION TIME(8,7)|UG G(8,3)|SUBSTANCE MERCURY(8,2)|ACCELERATE CHEMISORPTION(8,1)|MERCURY ARTIFICIAL EMISSION(8,1)|PARTICLE SIZE(7,7)|ROOM TEMPERATURE(7,7)|HIGH COST(7,4)|RECLAIMED RUBBER(7,2)|TIRE RETREADING(7,1)|WET DESULPHURIZATION(7,1)|COAL BURNING(6,1)|DESORPTION PHENOMENON(6,1)|FOREIGN COUNTRY(6,1)|GRADUALLY PAID ATTENTION(6,1)|GRANULAR MERCURY(6,1)|LITERATURE REPORT(6,1)|MERCURY PARTICLE(6,1)|SCRAP TIRE THERMAL DECOMPOSITION(5,2)|COAL COMBUSTION FLUE GAS(5,1)|SUBSTANCE ADSORPTION(5,1)|DEBACTEROL(4,2)|METHANE(4,2)|ACID DIPPING(4,1)|ACID SOAK(4,1)|BROMINE LOADING(4,1)|GASEOUS SUBSTANCE(4,1)|INORGANIC MATTER(4,1)|INORGANIC SALT(4,1)|ISOVOLUMETRIC HYDROGEN CHLORIDE(4,1)|MERCURY DISCHARGE(4,1)|MNCL2THE FORMATION(4,1)|NONNEGLIGIBLE ENVIRONMENTAL FACTOR(4,1)| (CN102580674)|1. A method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag is characterized by comprising the following steps: the method comprises the following operation steps:|1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|2) soaking 30-60 wt% hydrochloric acid or sulfuric acid aqueous solution into the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying at 110 ℃ for 48 hours;|3) and (3) activating the acid-impregnated pyrolysis residue by using high-temperature water vapor in a sealed furnace body under the nitrogen atmosphere, wherein the activation temperature is 800-1000 ℃, and the activation time is 1-3 hours, so that the mercury removing agent can be prepared. (CN102580674)|TECHNICAL FIELD|[0002] The invention relates to a flue gas demercuration technology, in particular to a method for preparing a demercuration agent by utilizing modified waste tire pyrolysis residues.|BACKGROUND ART|[0004] The energy structure of China is mainly based on coal, and the coal consumption is continuously increased. According to statistics, the capacity of the thermoelectric device accounts for more than 74% of the installed capacity of the power generation in China at present. The artificial emission of mercury worldwide is about 1000-. The research shows that: asia is the largest area of the world where man-made mercury emissions exceed 50% for the world. Coal combustion is considered by the literature to be one of the largest artificially emitted sources of mercury. China is a country with coal as a main energy source, and the coal burning becomes a non-negligible environmental factor for mercury discharge.|[0005] There are three forms of mercury in coal combustion flue gas: elemental mercury (Hg)0) Mercury (Hg) in its oxidized state2+E.g. HgCl2Or HgO) and particulate mercury (Hg)p). The mercury in the coal-fired flue gas mainly exists in the forms of elemental mercury and oxidized mercury, and the elemental mercury is the main form of the elemental mercury. In the high temperature region of the boiler, the mercury in the coal is released substantially as elemental mercury, and then in the rear, low temperature region, part of the mercury forms oxidized mercury (HgCl)2Or HgO). Since the granular mercury is generally enriched on the surface of the fly ash, most of the mercury can be removed by cloth bag dust removal or electric dust removal. The simple substance mercury in the flue gas, which is the main component, has limited capacity in the traditional adsorption method due to high volatility and low solubility. Compared with simple substance mercury, the oxidized mercury is easy to be absorbed, and meanwhile, the oxidized mercury has water solubility and can also be used in a subsequent wet desulphurization systemMost of it is removed. The mercury removal technology applied in the industry of developed countries in foreign countries at present is to spray activated carbon powder in a flue and adsorb mercury by using activated carbon, but the activated carbon spraying technology has the defects of high carbon consumption and high cost. However, general activated carbon mainly performs physical adsorption on mercury, and the adsorption capacity is limited.|[0006] Aiming at the modification of the activated carbon, a few literature reports exist at home and abroad, and research is carried out on loading technical oxides such as Ce, Cu, Mn and the like on the surface of the activated carbon, so that the adsorption capacity of the activated carbon on elemental mercury is improved, and the capacity of converting the individual elemental mercury into oxidized mercury is enhanced. It has also been shown that inorganic salts such as CaCl are added to the surface of activated carbon2、MgCl2、CoCl2、MnCl2The formation of various surface chemical groups has also been shown to accelerate the chemisorption of mercury onto activated carbon surfaces. Bromine loading can obviously increase the adsorption capacity of the activated carbon to the elemental mercury and accelerate the adsorption rate of the elemental mercury. However, most of these studies have been conducted on activated carbon.|[0007] The invention provides a method for adsorbing mercury in flue gas by modifying waste tires. With the rapid development of the automobile industry, the yield of waste tires in China is gradually increased. The current using modes of the waste tires include tire retreading, preparation of reclaimed rubber (rubber powder) and pyrolysis. The tire retreading and the preparation of reclaimed rubber (rubber powder) can only be carried out for limited times. Therefore, the thermal decomposition treatment of the waste tires is gradually paid attention in recent years, the thermal decomposition treatment of the waste tires can obtain fuel oil and carbon black, but the quality of the carbon black is poor, and the further industrial application of the technology is limited. The pyrolytic slag accounts for about 35 percent of the waste tires and belongs to solid slag which is difficult to utilize. The waste tire pyrolysis slag contains inorganic substances besides carbon, and the inorganic substances comprise elements such as Zn, Fe and S. Part of inorganic substances can be removed by using an acid dipping method, the specific surface area of the pyrolysis slag is increased, and meanwhile, part of substances contained in the pyrolysis slag, such as metal oxides, S and the like, are favorable for oxidation and adsorption of elemental mercury.|DISCLOSURE|[0008] Disclosure of Invention|[0009] The invention aims to provide a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis residues, aiming at the technical analysis, the mercury removing agent prepared by the method changes the pyrolysis residues into valuables, has the advantage of higher price than modified activated carbon, can obtain higher mercury removing rate, and the adsorption capacity of the modified pyrolysis residues to mercury reaches 800 ug/g.|[0010] The technical scheme of the invention is as follows:|[0011] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following operation steps:|[0012] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0013] 2) soaking 30-60 wt% hydrochloric acid or sulfuric acid aqueous solution into the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying at 110 ℃ for 48 hours;|[0014] 3) and (3) activating the acid-impregnated pyrolysis residue by using high-temperature water vapor in a sealed furnace body under the nitrogen atmosphere, wherein the activation temperature is 800-1000 ℃, and the activation time is 1-3 hours, so that the mercury removing agent can be prepared.|[0015] Technical analysis of the invention:|[0016] in the gas-solid heterogeneous catalytic reaction, gaseous substances are adsorbed on the surface of a material, and generally, the larger the specific surface area of the material is, the stronger the adsorption capacity is, under the same conditions. The invention adopts the waste tire pyrolysis residue to be subjected to acid soaking and high-temperature water vapor activation, and aims to improve the specific surface area and increase the mercury adsorption capacity. In addition, from the adsorption principle, the principle of physical adsorption and chemical adsorption exists on the surface of the adsorbent, the interaction force between physically adsorbed mercury and the surface of the material is relatively low, and the desorption phenomenon occurs after the temperature is slightly raised, so that the adsorption capacity is relatively low. However, if the surface of the catalytic adsorption material contains some ions or functional groups, the catalytic adsorption material can chemically react with the adsorbed substance, so that the mercury adsorption capacity and the mercury adsorption capacity can be improved. The scrap tire thermal decomposition residue is selected as a raw material because metal oxides such as Ze, Fe, etc., and S contained in the scrap tire thermal decomposition residue are advantageous for catalytic oxidation and adsorption of mercury. The method utilizes an isovolumetric hydrochloric acid and sulfuric acid dipping method to treat the pyrolysis residue, not only dissolves partial inorganic matters to increase the specific surface area, but also introduces Cl in the hydrochloric acid and S in the sulfuric acid to the surface of the adsorption material. These substances are advantageous for improving the chemisorption of mercury. High temperature steam activation is to further increase the specific surface area of the material.|[0017] In conclusion, the invention provides a method for modifying pyrolysis slag, which is a method for acid impregnation by an isometric method and then activation under high-temperature water vapor.|[0018] The invention has the advantages that: the prepared mercury removing agent for the modified pyrolysis slag changes the pyrolysis slag into valuable, has the advantage of higher price than modified activated carbon, and can obtain very high mercury removal rate, and the mercury adsorption capacity of the modified pyrolysis slag reaches 800 ug/g.|INVENTION MODE|[0019] Detailed Description|[0020] Some, but not all, examples are listed below:|[0021] example 1:|[0022] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following steps:|[0023] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0024] 2) soaking 60 wt% hydrochloric acid aqueous solution in the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying for 48 hours at 110 ℃;|[0025] 3) and (3) activating the acid-impregnated pyrolysis residues in a sealed furnace body under the nitrogen atmosphere by using high-temperature water vapor, wherein the activation temperature is 1000 ℃, and the activation time is 3 hours, so that the mercury removing agent is prepared.|[0026] The detection result shows that: the mercury removing agent has the adsorption capacity of 800ug/g for the mercury in the flue gas at the flue gas temperature of 100 ℃.|[0027] Example 2:|[0028] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following steps:|[0029] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0030] 2) soaking 30 wt% hydrochloric acid aqueous solution in the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying for 48 hours at 110 ℃;|[0031] 3) and (3) activating the acid-impregnated pyrolysis residues in a sealed furnace body under the nitrogen atmosphere by using high-temperature water vapor, wherein the activation temperature is 800 ℃, and the activation time is 1 hour, so that the mercury removing agent can be prepared.|[0032] The detection result shows that: the mercury removing agent has the adsorption capacity of 600ug/g for the mercury in the flue gas at the temperature of 200 ℃.|[0033] Example 3:|[0034] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following steps:|[0035] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0036] 2) soaking 60 wt% sulfuric acid aqueous solution in the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying for 48 hours at 110 ℃;|[0037] 3) and (3) activating the acid-impregnated pyrolysis residues in a sealed furnace body under the nitrogen atmosphere by using high-temperature water vapor, wherein the activation temperature is 1000 ℃, and the activation time is 3 hours, so that the mercury removing agent is prepared.|[0038] The detection result shows that: the mercury removing agent has the adsorption capacity of 760ug/g for the mercury in the flue gas at the temperature of 100 ℃.|[0039] Example 4:|[0040] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following steps:|[0041] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0042] 2) soaking a 30 wt% sulfuric acid aqueous solution in the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying for 48 hours at 110 ℃;|[0043] 3) and (3) activating the acid-impregnated pyrolysis residues in a sealed furnace body under the nitrogen atmosphere by using high-temperature water vapor, wherein the activation temperature is 800 ℃, and the activation time is 1 hour, so that the mercury removing agent can be prepared.|[0044] The detection result shows that: the mercury removing agent has the adsorption capacity of 560ug/g for the mercury in the flue gas at the temperature of 200 ℃. (CN102580674)|TECHNICAL FIELD|[0002] The invention relates to a flue gas demercuration technology, in particular to a method for preparing a demercuration agent by utilizing modified waste tire pyrolysis residues.|BACKGROUND ART|[0004] The energy structure of China is mainly based on coal, and the coal consumption is continuously increased. According to statistics, the capacity of the thermoelectric device accounts for more than 74% of the installed capacity of the power generation in China at present. The artificial emission of mercury worldwide is about 1000-. The research shows that: asia is the largest area of the world where man-made mercury emissions exceed 50% for the world. Coal combustion is considered by the literature to be one of the largest artificially emitted sources of mercury. China is a country with coal as a main energy source, and the coal burning becomes a non-negligible environmental factor for mercury discharge.|[0005] There are three forms of mercury in coal combustion flue gas: elemental mercury (Hg)0) Mercury (Hg) in its oxidized state2+E.g. HgCl2Or HgO) and particulate mercury (Hg)p). The mercury in the coal-fired flue gas mainly exists in the forms of elemental mercury and oxidized mercury, and the elemental mercury is the main form of the elemental mercury. In the high temperature region of the boiler, the mercury in the coal is released substantially as elemental mercury, and then in the rear, low temperature region, part of the mercury forms oxidized mercury (HgCl)2Or HgO). Since the granular mercury is generally enriched on the surface of the fly ash, most of the mercury can be removed by cloth bag dust removal or electric dust removal. The simple substance mercury in the flue gas, which is the main component, has limited capacity in the traditional adsorption method due to high volatility and low solubility. Compared with simple substance mercury, the oxidized mercury is easy to be absorbed, and meanwhile, the oxidized mercury has water solubility and can also be used in a subsequent wet desulphurization systemMost of it is removed. The mercury removal technology applied in the industry of developed countries in foreign countries at present is to spray activated carbon powder in a flue and adsorb mercury by using activated carbon, but the activated carbon spraying technology has the defects of high carbon consumption and high cost. However, general activated carbon mainly performs physical adsorption on mercury, and the adsorption capacity is limited.|[0006] Aiming at the modification of the activated carbon, a few literature reports exist at home and abroad, and research is carried out on loading technical oxides such as Ce, Cu, Mn and the like on the surface of the activated carbon, so that the adsorption capacity of the activated carbon on elemental mercury is improved, and the capacity of converting the individual elemental mercury into oxidized mercury is enhanced. It has also been shown that inorganic salts such as CaCl are added to the surface of activated carbon2、MgCl2、CoCl2、MnCl2The formation of various surface chemical groups has also been shown to accelerate the chemisorption of mercury onto activated carbon surfaces. Bromine loading can obviously increase the adsorption capacity of the activated carbon to the elemental mercury and accelerate the adsorption rate of the elemental mercury. However, most of these studies have been conducted on activated carbon.|[0007] The invention provides a method for adsorbing mercury in flue gas by modifying waste tires. With the rapid development of the automobile industry, the yield of waste tires in China is gradually increased. The current using modes of the waste tires include tire retreading, preparation of reclaimed rubber (rubber powder) and pyrolysis. The tire retreading and the preparation of reclaimed rubber (rubber powder) can only be carried out for limited times. Therefore, the thermal decomposition treatment of the waste tires is gradually paid attention in recent years, the thermal decomposition treatment of the waste tires can obtain fuel oil and carbon black, but the quality of the carbon black is poor, and the further industrial application of the technology is limited. The pyrolytic slag accounts for about 35 percent of the waste tires and belongs to solid slag which is difficult to utilize. The waste tire pyrolysis slag contains inorganic substances besides carbon, and the inorganic substances comprise elements such as Zn, Fe and S. Part of inorganic substances can be removed by using an acid dipping method, the specific surface area of the pyrolysis slag is increased, and meanwhile, part of substances contained in the pyrolysis slag, such as metal oxides, S and the like, are favorable for oxidation and adsorption of elemental mercury.|DISCLOSURE|[0008] Disclosure of Invention|[0009] The invention aims to provide a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis residues, aiming at the technical analysis, the mercury removing agent prepared by the method changes the pyrolysis residues into valuables, has the advantage of higher price than modified activated carbon, can obtain higher mercury removing rate, and the adsorption capacity of the modified pyrolysis residues to mercury reaches 800 ug/g.|[0010] The technical scheme of the invention is as follows:|[0011] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following operation steps:|[0012] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0013] 2) soaking 30-60 wt% hydrochloric acid or sulfuric acid aqueous solution into the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying at 110 ℃ for 48 hours;|[0014] 3) and (3) activating the acid-impregnated pyrolysis residue by using high-temperature water vapor in a sealed furnace body under the nitrogen atmosphere, wherein the activation temperature is 800-1000 ℃, and the activation time is 1-3 hours, so that the mercury removing agent can be prepared.|[0015] Technical analysis of the invention:|[0016] in the gas-solid heterogeneous catalytic reaction, gaseous substances are adsorbed on the surface of a material, and generally, the larger the specific surface area of the material is, the stronger the adsorption capacity is, under the same conditions. The invention adopts the waste tire pyrolysis residue to be subjected to acid soaking and high-temperature water vapor activation, and aims to improve the specific surface area and increase the mercury adsorption capacity. In addition, from the adsorption principle, the principle of physical adsorption and chemical adsorption exists on the surface of the adsorbent, the interaction force between physically adsorbed mercury and the surface of the material is relatively low, and the desorption phenomenon occurs after the temperature is slightly raised, so that the adsorption capacity is relatively low. However, if the surface of the catalytic adsorption material contains some ions or functional groups, the catalytic adsorption material can chemically react with the adsorbed substance, so that the mercury adsorption capacity and the mercury adsorption capacity can be improved. The scrap tire thermal decomposition residue is selected as a raw material because metal oxides such as Ze, Fe, etc., and S contained in the scrap tire thermal decomposition residue are advantageous for catalytic oxidation and adsorption of mercury. The method utilizes an isovolumetric hydrochloric acid and sulfuric acid dipping method to treat the pyrolysis residue, not only dissolves partial inorganic matters to increase the specific surface area, but also introduces Cl in the hydrochloric acid and S in the sulfuric acid to the surface of the adsorption material. These substances are advantageous for improving the chemisorption of mercury. High temperature steam activation is to further increase the specific surface area of the material.|[0017] In conclusion, the invention provides a method for modifying pyrolysis slag, which is a method for acid impregnation by an isometric method and then activation under high-temperature water vapor.|[0018] The invention has the advantages that: the prepared mercury removing agent for the modified pyrolysis slag changes the pyrolysis slag into valuable, has the advantage of higher price than modified activated carbon, and can obtain very high mercury removal rate, and the mercury adsorption capacity of the modified pyrolysis slag reaches 800 ug/g.|INVENTION MODE|[0019] Detailed Description|[0020] Some, but not all, examples are listed below:|[0021] example 1:|[0022] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following steps:|[0023] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0024] 2) soaking 60 wt% hydrochloric acid aqueous solution in the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying for 48 hours at 110 ℃;|[0025] 3) and (3) activating the acid-impregnated pyrolysis residues in a sealed furnace body under the nitrogen atmosphere by using high-temperature water vapor, wherein the activation temperature is 1000 ℃, and the activation time is 3 hours, so that the mercury removing agent is prepared.|[0026] The detection result shows that: the mercury removing agent has the adsorption capacity of 800ug/g for the mercury in the flue gas at the flue gas temperature of 100 ℃.|[0027] Example 2:|[0028] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following steps:|[0029] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0030] 2) soaking 30 wt% hydrochloric acid aqueous solution in the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying for 48 hours at 110 ℃;|[0031] 3) and (3) activating the acid-impregnated pyrolysis residues in a sealed furnace body under the nitrogen atmosphere by using high-temperature water vapor, wherein the activation temperature is 800 ℃, and the activation time is 1 hour, so that the mercury removing agent can be prepared.|[0032] The detection result shows that: the mercury removing agent has the adsorption capacity of 600ug/g for the mercury in the flue gas at the temperature of 200 ℃.|[0033] Example 3:|[0034] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following steps:|[0035] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0036] 2) soaking 60 wt% sulfuric acid aqueous solution in the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying for 48 hours at 110 ℃;|[0037] 3) and (3) activating the acid-impregnated pyrolysis residues in a sealed furnace body under the nitrogen atmosphere by using high-temperature water vapor, wherein the activation temperature is 1000 ℃, and the activation time is 3 hours, so that the mercury removing agent is prepared.|[0038] The detection result shows that: the mercury removing agent has the adsorption capacity of 760ug/g for the mercury in the flue gas at the temperature of 100 ℃.|[0039] Example 4:|[0040] a method for preparing a mercury removing agent by utilizing modified waste tire pyrolysis slag comprises the following steps:|[0041] 1) crushing the waste tire pyrolysis slag, wherein the particle size is 60-200 meshes;|[0042] 2) soaking a 30 wt% sulfuric acid aqueous solution in the waste tire pyrolysis residue in the same volume, continuously stirring for 1 hour at room temperature, and drying for 48 hours at 110 ℃;|[0043] 3) and (3) activating the acid-impregnated pyrolysis residues in a sealed furnace body under the nitrogen atmosphere by using high-temperature water vapor, wherein the activation temperature is 800 ℃, and the activation time is 1 hour, so that the mercury removing agent can be prepared.|[0044] The detection result shows that: the mercury removing agent has the adsorption capacity of 560ug/g for the mercury in the flue gas at the temperature of 200 ℃. Family Number|(7775753)|7775753|Abstract|(CN102580674B B)|The invention discloses a method for preparing a mercury removal agent by utilizing a modified waste tire pyrolysis residue . The method comprises the following steps : ( 1 ) crushing the waste tire pyrolysis residue , wherein the particle sizes of particles are 60-200 meshes ; ( 2 ) immersing hydrochloric acid or sulfuric acid water solution with the concentration of 30-60 wt % into the waste tire pyrolysis residue in an isovolumetric manner , continuously stirring for 1 h at room temperature , then drying for 48 h at a temperature of 110 DEG C ; and ( 3 ) activating the pyrolysis residue subjected to the acid immersion in a sealed furnace body in the atmosphere of nitrogen by using high - temperature vapor at a temperature of 800-1000 DEG C for 1-3 h so as to obtain the mercury removal agent . The method has the advantages that : the mercury removal agent prepared by the modified pyrolysis residue enables the pyrolysis residue to become profitable , the price of the modified pyrolysis residue is lower than that of the modified active carbon , high mercury removal rate can be achieved at the same time , and the adsorption capacity of the modified pyrolysis residue for mercury is up to 800 mug / g . |IPC codes|(CN102580674B B)|B01D - 053/02 |B01D - 053/64 |B01D - 053/86 |B01J - 020/20 |B01J - 020/30 |B01J - 027/138 | Chemical engineering|Environmental technology B01D-053/02|B01D-053/64|B01D-053/86|B01J-020/20|B01J-020/30|B01J-027/138 B01D-053/02|B01D-053/64|B01D-053/86|B01J-020/20|B01J-020/30|B01J-027/138 CN110013828B|CN109517611|CN117504819B|CN114433019B|CN102728321B CN110013828B 85373652 WHO=Examiner SELF=N CAT=A|CN109517611 83906555 WHO=Examiner SELF=N CAT=A|CN117504819B 108414673 WHO=Examiner SELF=N|CN114433019B 99917310 WHO=Examiner SELF=N|CN102728321B 7885449 WHO=Examiner SELF=N CN101164876|CN1944581 CN101164876 6523840 WHO=Examiner SELF=Y CAT=X|CN1944581 5376016 WHO=Examiner SELF=N CAT=A CN101164876; CN1944581 LAPSED (CN102580674)|LAPSED DEAD (CN102580674)|DEAD (CN102580674)|LEGAL DETAILS FOR CN102580674|Actual or expected expiration date=2014-02-21|Legal state=DEAD|Status=LAPSED|Event publication date=2012-02-21|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201210039920|Application date=2012-02-21|Standardized application number=2012CN-0039920|Event publication date=2012-07-18|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN102580674|Publication stage code=A|Publication date=2012-07-18|Standardized publication number=CN102580674|Event publication date=2012-07-18|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2012-09-19|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2013-08-14|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN102580674|Publication stage code=B|Publication date=2013-08-14|Standardized publication number=CN102580674B|Event publication date=2013-08-14|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2015-04-08|Event code=CN/CF01|Event indicator=Neg|Event group=Event indicating Not In Force|Termination of patent right due to non-payment of annual fee|Effective date of the event=2014-02-21 https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjn+xoquSCrePxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=048mTd1NEVfjx8oIHuCdw7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN102580674)|NAME=HOU LI;TIANJIN JIAMENG INTETTECTUAL PROPERTY AGENT CO. LTD.|(CN102580674)|NAME=HOU LI;TIANJIN JIAMENG INTETTECTUAL PROPERTY AGENT CO. LTD. (CN102580674)|NAME=SHEN BOXIONG|(CN102580674)|NAME=SHEN BOXIONG 0 1 Titre: (CN102580674)|Method for preparing mercury removal agent by utilizing modified waste tire pyrolysis residue Résumé: (CN102580674)|The invention discloses a method for preparing a mercury removal agent by utilizing a modified waste tire pyrolysis residue. The method comprises the following steps: (1) crushing the waste tire pyrolysis residue, wherein the particle sizes of particles are 60-200 meshes; (2) immersing hydrochloric acid or sulfuric acid water solution with the concentration of 30-60wt% into the waste tire pyrolysis residue in an isovolumetric manner, continuously stirring for 1h at room temperature, then drying for 48h at a temperature of 110 DEG C; and (3) activating the pyrolysis residue subjected to the acid immersion in a sealed furnace body in the atmosphere of nitrogen by using high-temperature vapor at a temperature of 800-1000 DEG C for 1-3h so as to obtain the mercury removal agent. The method has the advantages that: the mercury removal agent prepared by the modified pyrolysis residue enables the pyrolysis residue to become profitable, the price of the modified pyrolysis residue is lower than that of the modified active carbon, high mercury removal rate can be achieved at the same time, and the adsorption capacity of the modified pyrolysis residue for mercury is up to 800 mug/g. 103 Abstract gpt-4o-mini no The article focuses on a method for preparing a mercury removal agent from waste tire pyrolysis residue, which does not relate to accelerated weathering or CO₂ capture.
107 CN202010926200 CN202010926200 CN112010302 91712277 CN112010302 A 2020-12-01 [CN112010302] 2020-09-07 2020-09-07 2020-12-01 (CN112010302)|2022-12-23 (CN112010302)|Method for preparing hierarchical-pore phosphorus-doped carbon material from biomass (CN112010302)|The invention relates to a method for preparing a hierarchical-pore phosphorus-doped carbon material from biomass. The method comprises the following steps: firstly, crushing the biomass into tiny particles; then uniformly mixing the crushed biomass particles with a phosphoric acid-containing solution according to a certain ratio to form a mixture; putting the mixture into a hydrothermal reactionkettle, and carrying out a hydrothermal reaction at a certain temperature to generate hydrothermal carbon; dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction; andputting the dried hydrothermal carbon into a pyrolyzing furnace, and carrying out rapid pyrolysis under the protection of an inert atmosphere to obtain a hierarchical-pore phosphorus-doped carbon material after rapid pyrolysis. According to the method disclosed by the invention, a rapid pyrolysis scheme is combined with phosphoric acid hydrothermal pre-carbonization, so a very ideal effect can beachieved only by performing rapid pyrolysis in a very short time, carbon preparation efficiency is greatly improved, and energy consumption is remarkably reduced; and meanwhile, due to the existence of phosphorus, a good carbon sequestration effect can be achieved, and carbon yield is increased. HEFEI UNIVERSITY OF TECHNOLOGY (CN112010302)|HEFEI UNIVERSITY OF TECHNOLOGY ([CN]) MA PEIYONG|LIN FENGFEI|ZHANG YING|LIU XIAOHAO|HUANG RUIYI|QI FENGLEI|XING XIANJUN (CN112010302)|MA PEIYONG|LIN FENGFEI|ZHANG YING|LIU XIAOHAO|HUANG RUIYI|QI FENGLEI|XING XIANJUN (CN112010302)|HONG LING;HEFEI ZHONGGU INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 34146 (CN112010302)|However, due to high labor cost, low economic benefit and increasingly strict environmental regulations, the recycling of the biomass is not widely promoted at present, and most of the biomass is directly discarded; the carbon material has the characteristics of good surface chemical property, excellent mechanical stability, rich pore channels, excellent conductivity and the like, and shows great advantages and potentials in the aspects of catalysis, hydrogen storage, separation and adsorption, electrochemistry and the like.|in addition, the process method of phosphoric acid hydrothermal combined fast pyrolysis can overcome the problems of limited specific surface area, large ash content, low and uneven heteroatom doping amount, low carbon yield and the like of the activated carbon prepared by the traditional method; and the phosphorus not doped into the activated carbon can be recycled by washing, no phosphoric acid is discharged in the whole preparation process, the method has obvious advantages in the aspects of energy and environment, the whole process is green, simple and efficient, the raw material source is wide, and the method can be used for large-scale production.|(2) Post-treatment doping method: the method generally refers to introducing a functional group containing phosphorus atoms into an activated carbon material through surface modification such as a dry method or a wet method, and the like, and the method may cause structural collapse of the activated carbon material, so that the specific surface area of the activated carbon material is reduced, and the activated carbon material is difficult to uniformly dope the phosphorus atoms due to stable chemical properties.| (CN112010302)|1. A method for preparing a hierarchical porous phosphorus-doped carbon material by biomass is characterized by comprising the following steps: the method comprises the following steps:crushing biomass into tiny particles;step two, uniformly mixing the crushed biomass particles with a phosphorus-containing acidic solution in proportion to form a mixture;step three, carrying out hydrothermal reaction on the mixture to generate hydrothermal carbon;step four, dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction;and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, and performing fast pyrolysis under the protection of inert atmosphere to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.| (CN112010302)|The invention provides a method for converting agriculture and forestry biomass waste into a phosphorus-doped hierarchical porous carbon material by utilizing a phosphoric acid hydrothermal pretreatment combined fast pyrolysis technology, wherein the process is characterized in that the hydrothermal method and the fast pyrolysis method are not simply superposed, but acid, hydrothermal and fast pyrolysis are mutually coupled, so that a remarkable synergistic effect is achieved;|The invention relates to a method for preparing a hierarchical porous phosphorus-doped carbon material by biomass, which comprises the following steps: firstly, crushing biomass into tiny particles; then uniformly mixing the crushed biomass particles with a phosphorus-containing acidic solution according to a certain proportion to form a mixture; putting the mixture into a hydrothermal reaction kettle, and carrying out hydrothermal reaction at a certain temperature to generate hydrothermal carbon; dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction; putting the dried hydrothermal carbon into a pyrolysis furnace, and performing fast pyrolysis under the protection of inert atmosphere to obtain a fast pyrolyzed hierarchical porous phosphorus-doped carbon material; the invention selects the scheme of fast pyrolysis to combine with the phosphoric acid hydrothermal pre-carbonization, thus achieving very ideal effect only by fast pyrolysis in a very short time, greatly improving the carbon production efficiency and simultaneously obviously reducing the energy consumption; meanwhile, the existence of phosphorus can play a good role in carbon fixation, and the carbon yield is improved.| (CN112010302)|BIOMASS(100,38)|FAST PYROLYSIS(100,36)|CARBON(100,32)|CRUSHED BIOMASS PARTICLE(99,11)|CRUSHING BIOMASS(94,5)|HYDROTHERMAL CARBON(81,29)|HYDROTHERMAL PRECARBONIZATION(78,5)|PYROLYSIS FURNACE(75,10)|TINY PARTICLE(73,4)|LIGNOCELLULOSE BIOMASS(72,6)|PHOSPHORIC ACID HYDROTHERMAL PRECARBONIZATION(64,4)|DRIED HYDROTHERMAL CARBON(63,10)|PHOSPHORUS EXISTENCE(59,3)|ACIDIC SOLUTION(46,12)|JATROPHA CURCAS CAKE(44,3)|HYDROTHERMAL REACTION KETTLE(41,10)|JACKFRUIT PEEL(40,3)|HYDROTHERMAL REACTION(39,29)|PHOSPHORUS(38,24)|INERT ATMOSPHERE PROTECTION(38,9)|ARTICHOKE LEAF(37,3)|PEACH KERNEL(37,3)|RAPESEED CAKE(37,3)|SMOOTH CORD GRASS(37,3)|OLIVE KERNEL(36,3)|COTTON STALK(35,3)|CORN STALK(32,3)|ALMOND SHELL(31,3)|LOTUS STEM(31,3)|PECAN SHELL(31,3)|PEANUT SHELL(30,3)|REED LEAF(30,3)|CARBON PRODUCTION(29,3)|DATE KERNEL(29,3)|CARBON YIELD(26,4)|PROTEIN RESIDUE(26,3)|AGRICULTURAL SOLID WASTE(25,6)|BAGASSE(25,6)|NA2HPO4(25,3)|NAH2PO4(25,3)|CRUSHING WOOD CHIP BIOMASS(24,6)|FAST PYROLYSIS FURNACE(24,6)|INERT ATMOSPHERE(23,10)|HIERARCHIC PORE PHOSPHORUS(22,3)|HEMICELLULOSE(20,4)|APRICOT KERNEL(20,3)|DEBACTEROL(20,3)|MONOAMMONIUM PHOSPHATE(20,3)|MOSO BAMBOO(20,3)|CARBON FIXATION(19,3)|CELLOBIOSE(19,3)|DIPOTASSIUM PHOSPHATE(19,3)|MICROALGAE(19,3)|AMMONIUM POLYPHOSPHATE(18,3)|CHITOSAN(18,3)|FRUCTOSE(17,3)|URBAN SOLID WASTE(17,3)|PHOSPHORIC ACID(16,34)|PHOSPHORUS MIXING RATIO(16,2)|CHITIN(15,3)|FRUIT PULP(15,3)|LIGNIN(15,3)|PHOSPHORUS DOPED BIOMASS(15,3)|RICE HULL(15,3)|XYLAN(15,3)|XYLOSE(15,3)|HUGE RESOURCE TREASURY(15,1)|RENEWABLE BIOMASS RESOURCE(15,1)|CARBON MATERIAL(14,49)|INORGANIC ACID(14,9)|PHOSPHORIC ACID HYDROTHERMAL CARBON(14,6)|COCONUT SHELL(14,3)|CORN COB(14,3)|GLUCOSE(14,3)|CATALYZING BIOMASS HYDROLYSIS(14,1)|HEMP(13,3)|STARCH(13,3)|STEP FIVE(13,1)|ENERGY CONSUMPTION(12,5)|ANIMAL WASTE(12,3)|CALCIUM PHOSPHATE(12,3)|COFFEE GROUND(12,3)|HAY(12,3)|PHOSPHORIC ACID AQUEOUS SOLUTION(12,3)|BIOMASS RESIDUE(12,2)|POWER STRUCTURE PORE(12,2)|BEAKER(11,7)|DEHYDRATION(11,7)|SODIUM PHOSPHATE(11,3)|STEP FOUR(11,2)|BIOMASS FEEDSTOCK(11,1)|MICROWAVE CARBONIZATION(11,1)|QUICK CARBOMORPHISM ACTIVATION(11,1)|FAST COOLING(10,6)|OPTIMIZATION(10,6)|MEPH2 RATIO(10,3)|CLEANING OKRA(10,2)|WASTE BIOMASS(10,2)|ACID HYDROTHERMAL PRETREATMENT(10,1)|BIOMASS ASH OXIDE(10,1)|BIOMASS CARBONIZATION REACTION(10,1)|PHOSPHORUS ATOM DOPING(10,1)|RESEARCH HOTSPOT(10,1)|SYNCHRONOUS DEASHING(10,1)|FORMIC ACID(9,3)|HYDROGEN CHLORIDE(9,3)|OXALIC ACID(9,3)|WASTE PAPER(9,3)|WATER HYACINTH(9,3)|PHOSPHORUS SOURCE(8,4)|ACETIC ACID(8,3)|MUNICIPAL SOLID WASTE(8,3)|PLASTIC WASTE(8,3)|PHOSPHORIC ACID FAST PYROLYSIS(8,2)|BIOMASS ASH COMPONENT(8,1)|DEEP CARBONIZATION(8,1)|GRADUAL ENERGY EXHAUSTION(8,1)|RAPID PYROLYSIS(8,1)|RESOURCE SHORTAGE CONDITION(8,1)|PHOSPHORUS DOPED CARBON MATERIAL(7,16)|PHOSPHORIC ACID SOLUTION(7,7)|PHOSPHORUS CARBON MASS RATIO(7,3)|7A PHOSPHORUS(7,1)|ADSORPTION CAPACITY(7,1)|BIOMASS WASTE(7,1)|BLACK FOAM CARBONIZATION PRODUCT(7,1)|CARRYING OUT HYDROTHERMAL REACTION(7,1)|DRIED BIOMASS(7,1)|FAST PYROLYSIS REACTION(7,1)|FAST PYROLYSIS TARGET PRODUCT(7,1)|FREEZE DRYING OKRA(7,1)|HUNDRED MILLION TON(7,1)|MICROPOROUS MESOPOROUS CARBON(7,1)|NITROGEN ADSORPTION DESORPTION(7,1)|NUMEROUS INSUBSTANTIAL MODIFICATION(7,1)|PHOSPHORUS INTRODUCTION(7,1)|XPS SPECTRUM(7,1)|RED FUMING NITRIC ACID(6,3)|STRAW(5,2)|ACID COOKING(5,1)|ATMOSPHERIC ATMOSPHERE(5,1)|BIOMASS DELIMING SYNERGISTIC OPERATION(5,1)|BLACK SOLID POWDER(5,1)|CARBON SKELETON COLLAPSE(5,1)|CARBONIZED PRODUCT(5,1)|ELECTROCHEMISTRY(5,1)|FREEZE DRIED OKRA(5,1)|MAJOR CATEGORY(5,1)|PHOSPHORUS DOPING AGENT(5,1)|PHYTATE SOLUTION(5,1)|PRECARBONIZATION(5,1)|SOAKING SOLUTION(5,1)| (CN112010302)|1. A method for preparing a hierarchical porous phosphorus-doped carbon material by biomass is characterized by comprising the following steps: the method comprises the following steps:|crushing biomass into tiny particles;|step two, uniformly mixing the crushed biomass particles with a phosphorus-containing acidic solution in proportion to form a mixture;|step three, carrying out hydrothermal reaction on the mixture to generate hydrothermal carbon;|step four, dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction;|and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, and performing fast pyrolysis under the protection of inert atmosphere to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|2. The method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 1, wherein the method comprises the following steps: in the step one, the biomass is any one or the combination of more than two of lignocellulose biomass, agricultural solid waste and municipal solid waste; the lignocellulose biomass comprises cellulose, lignin, xylose, xylan, glucose, cellobiose, starch, hemicellulose, chitosan, chitin, sucrose and fructose; coconut shell, olive kernel, apricot kernel, date kernel, peach kernel, almond shell, pecan shell, peanut shell, corn cob, Muricius seed, fruit pulp, wood, bagasse, moso bamboo, corn stalk, cotton stalk, hemp, rice hull, jackfruit peel, coffee grounds, smooth cord grass, bagasse, artichoke leaf, reed leaf, lotus stem, water hyacinth, hay, microalgae; the agricultural solid waste comprises rapeseed cakes, jatropha curcas cakes, cake pulp, vinasse, waste protein and animal waste, and the urban solid waste comprises waste paper, plastic waste and regenerated plastic.|3. The method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 1, wherein the method comprises the following steps: and in the second step, the phosphorus-containing acidic solution is a phosphoric acid aqueous solution or an acidic phosphate solution.|4. The method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 3, wherein the method comprises the following steps: the acidic phosphate solution is any one of a solution formed by acidic phosphate and inorganic acid, a solution formed by acidic phosphate and organic acid, a solution formed by non-acidic phosphate and inorganic acid and a solution formed by non-acidic phosphate and organic acid, the acidic phosphate comprises dipotassium hydrogen phosphate, sodium dihydrogen phosphate and ammonium dihydrogen phosphate, the non-acidic phosphate comprises disodium hydrogen phosphate, sodium phosphate, potassium phosphate, calcium phosphate and ammonium polyphosphate, the inorganic acid comprises hydrochloric acid, sulfuric acid, phosphoric acid and nitric acid, and the organic acid comprises formic acid, acetic acid, citric acid and oxalic acid.|5. The method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 1, wherein the method comprises the following steps: and in the second step, the mixing ratio of the phosphorus-containing acidic solution and the biomass particles is controlled to be between 0.1:1 and 5:1 according to the phosphorus/carbon mass ratio.|6. The method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 1, wherein the method comprises the following steps: the temperature of the hydrothermal reaction in the third step is 70-300 ℃.|7. The method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 1, wherein the method comprises the following steps: the hydrothermal reaction time in the third step is 1-24 h.|8. The method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 1, wherein the method comprises the following steps: the temperature of the fast pyrolysis in the step five is 350-1000 ℃,|9. the method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 8, wherein the method comprises the following steps: the temperature of the fast pyrolysis in the fifth step is preferably 450-800 ℃.|10. The method for preparing the hierarchical porous phosphorus-doped carbon material from the biomass according to claim 1, wherein the method comprises the following steps: and the time for fast pyrolysis in the fifth step is 5 min. (CN112010302)|TECHNICAL FIELD|[0002] The invention belongs to the field of preparation of phosphorus-doped carbon materials, and particularly relates to the field of preparation of a hierarchical porous phosphorus-doped carbon material by using biomass.|BACKGROUND ART|[0004] Biomass is the world's fourth largest energy source second only to coal, oil and gas, accounting for approximately 14% of the world's primary energy consumption. China produces approximately 24 million tons of waste biomass (crop straw, wood chips, weeds, etc.) per year. The energy sources stored in the waste biomasses are equivalent to 10 hundred million tons of standard coal, and the waste biomasses are a huge resource treasury. However, due to high labor cost, low economic benefit and increasingly strict environmental regulations, the recycling of the biomass is not widely promoted at present, and most of the biomass is directly discarded; the carbon material has the characteristics of good surface chemical property, excellent mechanical stability, rich pore channels, excellent conductivity and the like, and shows great advantages and potentials in the aspects of catalysis, hydrogen storage, separation and adsorption, electrochemistry and the like. Under the conditions of current resource shortage, gradual energy exhaustion and environmental deterioration, biomass wastes (such as various straws, chaffs, wood chips and the like) rich in resources are used as raw materials to prepare activated carbon, namely biomass-based activated carbon, which is considered to be one of the most effective modes for utilizing waste biomass; in recent years, in order to further improve the application of carbon materials in catalysis, adsorption, sensing, electrochemistry and the like, the achievement of unique performance of carbon materials through surface and structure modification is one of the research hotspots in recent years, and many scholars have increased research on phosphorus-doped carbon materials, compared with pure carbon materials, phosphorus-containing carbon materials contain hydrophilic acid surfaces and chemical stability, show high adsorption capacity on basic metal ions and organic molecules, and have good catalytic activity in various reactions.|[0005] Currently, methods for introducing phosphorus into carbon structures can be divided into three major categories:|[0006] (1) carrying out heat treatment after physically mixing or chemically bonding the carbon-containing precursor and the phosphorus-containing compound: the method is characterized in that a carbon-containing precursor and a phosphorus-containing compound are mixed and then carbonized, or the carbon-containing precursor and the phosphorus-containing compound are reacted to obtain a phosphorus-containing organic substance and then carbonized, and phosphorus atoms are introduced into a carbon skeleton in the carbonization process. This method is simple in process, but generally costly using an organic carbon precursor and a phosphorus-containing ligand.|[0007] (2) Post-treatment doping method: the method generally refers to introducing a functional group containing phosphorus atoms into an activated carbon material through surface modification such as a dry method or a wet method, and the like, and the method may cause structural collapse of the activated carbon material, so that the specific surface area of the activated carbon material is reduced, and the activated carbon material is difficult to uniformly dope the phosphorus atoms due to stable chemical properties.|[0008] (3) Vapor deposition of carbon and phosphorus: the method refers to the phosphorus-containing carbon prepared by forming solid substances deposited on a substrate through gas-phase chemical reaction between gaseous carbon-containing and phosphorus-containing compounds at medium temperature or high temperature, and the chemical reaction can be promoted by adopting plasma and laser auxiliary technology, so that the deposition can be carried out at lower temperature. The method has high requirements on equipment, high price, high technical requirements and difficult operation.|[0009] In recent years, some inventions have disclosed methods for producing phosphorus-doped carbon materials, but these methods are clearly different from the present invention. Such as the following prior patents:|[0010] a) CN 201710764307.2A preparation method and application of a phosphorus-doped biomass graded porous carbon material, the patent relates to the preparation of a phosphorus-doped biomass graded porous carbon material, and the preparation method comprises the following steps: the dried biomass is first crushed and then soaked in phytate solution for several hours. And then carrying out constant-temperature heat treatment for 1-10 h at 500-1000 ℃ under the protection of inert gas. Performing acid cooking and water cooking to remove impurities, and drying to obtain a phosphorus-doped biomass graded porous carbon material with the specific surface area of 800-2100 cm 2/g; the preparation method related in the patent is a one-step high-temperature direct carbonization method, is different from the method of combining hydrothermal pretreatment and fast pyrolysis of phosphoric acid in the patent, takes phosphorus-containing organic salt substances as a template agent, a phosphorus doping agent and a pore-forming agent, and is different from the phosphoric acid solution used in the patent. The phosphoric acid hydrothermal method has a certain phosphorus doping effect, and simultaneously has the effects of catalyzing biomass hydrolysis, carbonization, pore forming, ash removal and the like, so that the preparation of a high-performance carbon material is facilitated; although the multi-level pore material can be obtained by the patent, the pyrolysis time is longer, and the phosphorus doping amount is lower.|[0011] b) CN 201710171948.7A phosphorus doped mesoporous carbon material and a microwave preparation method thereof, the patent relates to a preparation method of the phosphorus doped mesoporous carbon material, the preparation method comprises the following steps: putting 6-10 g of phytic acid into an open quartz reactor, and then putting the quartz reactor into a microwave oven; heating for 1-5 minutes under an atmospheric atmosphere at the microwave power of 400-800W to obtain a black foam carbonization product; then soaking the carbonized product in 100mL of acid liquor with the mass percentage concentration of 1-4% for 1-4 hours at room temperature; filtering the soaking solution, and filtering and washing the solid with clear water until the pH value of the filtrate is neutral to obtain black powdery solid; drying the black powdery solid for 8-12 hours at the temperature of 80-120 ℃ to obtain the phosphorus-doped mesoporous carbon material; the preparation method directly takes the phosphorus-rich organic matter phytic acid as a precursor, but not biomass wastes, has higher cost and limited phosphorus doping rate, is a microwave carbonization method, and is different from the method combining hydrothermal pretreatment and fast pyrolysis of phosphoric acid;|[0012] c) CN 201810591723.1A phosphorus-doped microporous/mesoporous carbon material and a preparation method thereof, the patent relates to a preparation method of the phosphorus-doped microporous/mesoporous carbon material, the preparation method of the microporous/mesoporous carbon material comprises the following steps of cleaning okra with clear water, drying, and freeze-drying at-45 to-80 ℃ for 48 to 96 hours to obtain freeze-dried okra; then carrying out heat treatment for 2-4 hours at 700-900 ℃ to obtain a phosphorus-doped microporous/mesoporous carbon material; the pretreatment method related in the patent is low-temperature freeze-drying okra, is different from the acid hydrothermal pretreatment method in the patent, cannot realize synchronous deashing, acid loading and pre-carbonization, cannot promote the carbonization process and shorten the treatment time; the used raw materials are okra which can be used, but biomass waste is not used, so that the cost is high; the heat treatment is carried out for 2 to 4 hours at high temperature, the time consumption is long, the energy consumption is large, and the specific surface area of the prepared carbon material is small.|DISCLOSURE|[0013] Disclosure of Invention|[0014] In order to solve the problems, the invention achieves the purposes through the following technical scheme:|[0015] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0016] crushing biomass into tiny particles;|[0017] step two, uniformly mixing the crushed biomass particles and the phosphorus-containing acidic solution in proportion to form a mixture;|[0018] step three, placing the mixture into a hydrothermal reaction kettle, and carrying out hydrothermal reaction at a certain temperature to generate hydrothermal carbon;|[0019] step four, dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction;|[0020] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, and performing fast pyrolysis under the protection of inert atmosphere to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0021] As a further optimized scheme of the invention, in the first step, the biomass is any one or a combination of more than two of lignocellulose biomass, agricultural solid waste and municipal solid waste; the lignocellulose biomass comprises cellulose, lignin, xylose, xylan, glucose, cellobiose, starch, hemicellulose, chitosan, chitin, sucrose and fructose; coconut shell, olive kernel, apricot kernel, date kernel, peach kernel, almond shell, pecan shell, peanut shell, corn cob, Muricius seed, fruit pulp, wood, bagasse, moso bamboo, corn stalk, cotton stalk, hemp, rice hull, jackfruit peel, coffee grounds, smooth cord grass, bagasse, artichoke leaf, reed leaf, lotus stem, water hyacinth, hay, microalgae; the agricultural solid waste comprises rapeseed cakes, jatropha curcas cakes, cake pulp, vinasse, waste protein and animal waste, and the urban solid waste comprises waste paper, plastic waste and regenerated plastic.|[0022] As a further optimized scheme of the invention, the phosphorus-containing acidic solution in the second step is a phosphoric acid aqueous solution or an acidic phosphate solution.|[0023] As a further optimized scheme of the present invention, the acidic phosphate solution is any one of a solution formed by acidic phosphate and inorganic acid, a solution formed by acidic phosphate and organic acid, a solution formed by non-acidic phosphate and inorganic acid, and a solution formed by non-acidic phosphate and organic acid, the acidic phosphate includes dipotassium hydrogen phosphate, sodium dihydrogen phosphate, and ammonium dihydrogen phosphate, the non-acidic phosphate includes disodium hydrogen phosphate, sodium phosphate, potassium phosphate, calcium phosphate, and ammonium polyphosphate, the inorganic acid includes hydrochloric acid, sulfuric acid, phosphoric acid, and nitric acid, and the organic acid includes formic acid, acetic acid, citric acid, and oxalic acid.|[0024] As a further optimization scheme of the invention, the mixing ratio of the phosphorus-containing acidic solution and the biomass particles in the second step is controlled to be between 0.1:1 and 5:1 according to the phosphorus/carbon mass ratio.|[0025] As a further optimization scheme of the invention, the temperature of the hydrothermal reaction in the third step is 70-300 ℃.|[0026] As a further optimization scheme of the invention, the time of the hydrothermal reaction in the third step is 1-24 h.|[0027] As a further optimization scheme of the invention, the temperature of the fast pyrolysis in the fifth step is 350-1000 ℃.|[0028] As a further optimization scheme of the invention, the temperature of the fast pyrolysis in the fifth step is preferably 450-800 ℃.|[0029] As a further optimization scheme of the invention, the time for fast pyrolysis in the fifth step is 5 min.|[0030] The invention has the beneficial effects that:|[0031] 1) the invention selects the scheme of fast pyrolysis to combine with the phosphoric acid hydrothermal pre-carbonization, thus achieving very ideal effect only by fast pyrolysis in a very short time, greatly improving the carbon production efficiency and simultaneously obviously reducing the energy consumption; meanwhile, the existence of phosphorus can play a good role in carbon fixation, so that the carbon yield is improved;|[0032] 2) according to the invention, renewable biomass resources with wide sources are used as carbon sources, and the raw materials are clean and low in price;|[0033] 3) the phosphoric acid in the invention can be used as a phosphorus source to be doped into the carbon material and also can be used as an activating agent, so that synchronous pore-forming and phosphorus atom doping can be realized, and the doping amount is higher;|[0034] 4) the production process method is simple, convenient and feasible, short in time consumption and low in energy consumption, and is suitable for large-scale production.|DRAWINGS DESCRIPTION|[0036] FIG. 1 is an XPS spectrum of the phosphorus element of the phosphorus-doped carbon material of the present invention;|[0037] FIG. 2 is a nitrogen adsorption/desorption isotherm of a phosphorus-doped carbon material according to the present invention;|[0038] FIG. 3 is a TEM image of a phosphorus-doped carbon material according to the present invention;|[0039] FIG. 4 shows the results of nitrogen desorption tests of the phosphorus-doped carbon material of the present invention;|[0040] FIG. 5 is a flow chart of the steps of the manufacturing process of the present invention;|INVENTION MODE|[0041] Detailed Description|[0042] The present application will now be described in further detail with reference to the drawings, it should be noted that the following detailed description is given for illustrative purposes only and is not to be construed as limiting the scope of the present application, as those skilled in the art will be able to make numerous insubstantial modifications and adaptations to the present application based on the above disclosure.|[0043] A method for preparing a hierarchical porous phosphorus-doped carbon material from biomass as shown in fig. 1 to 5 comprises the following steps: the method comprises the following steps:|[0044] crushing biomass into tiny particles;|[0045] wherein, the biomass in the first step of the biomass is any one or the combination of more than two of lignocellulose biomass, agricultural solid waste and municipal solid waste; the lignocellulose biomass comprises cellulose, lignin, xylose, xylan, glucose, cellobiose, starch, hemicellulose, chitosan, chitin, sucrose and fructose; coconut shell, olive kernel, apricot kernel, date kernel, peach kernel, almond shell, pecan shell, peanut shell, corn cob, Muricius seed, fruit pulp, wood, bagasse, moso bamboo, corn stalk, cotton stalk, hemp, rice hull, jackfruit peel, coffee grounds, smooth cord grass, bagasse, artichoke leaf, reed leaf, lotus stem, water hyacinth, hay, microalgae; the agricultural solid waste comprises rapeseed cakes, jatropha curcas cakes, cake pulp, vinasse, waste protein and animal waste, and the urban solid waste comprises waste paper, plastic waste and regenerated plastic;|[0046] step two, mixing the crushed biomass particles with a phosphorus-containing acidic solution according to a phosphorus/carbon mass ratio of 0.1:1 to 5:1 to form a uniform mixture; in the process, the synergistic operation of biomass deliming, pore-forming, phosphoric acid loading and pre-carbonization is realized;|[0047] wherein the phosphorus-containing acidic solution is phosphoric acid aqueous solution or acidic phosphate solution,|[0048] the acidic phosphate solution is any one of a solution formed by acidic phosphate and inorganic acid, a solution formed by acidic phosphate and organic acid, a solution formed by non-acidic phosphate and inorganic acid and a solution formed by non-acidic phosphate and organic acid;|[0049] the acidic phosphate comprises dipotassium hydrogen phosphate, sodium dihydrogen phosphate, and ammonium dihydrogen phosphate;|[0050] the non-acidic phosphate comprises disodium hydrogen phosphate, sodium phosphate, potassium phosphate, calcium phosphate, and ammonium polyphosphate;|[0051] the inorganic acid comprises hydrochloric acid, sulfuric acid, phosphoric acid, and nitric acid;|[0052] the organic acid includes formic acid, acetic acid, citric acid, oxalic acid;|[0053] step three, placing the mixture into a hydrothermal reaction kettle, and controlling the temperature of the hydrothermal reaction to be 70-300 ℃ to carry out hydrothermal reaction to generate hydrothermal carbon; and the time of the hydrothermal reaction is 1h to 24 h;|[0054] step four, dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction;|[0055] putting the dried hydrothermal carbon into a pyrolysis furnace, and performing fast pyrolysis in the presence of inert atmosphere for 5min to obtain a fast pyrolyzed hierarchical porous phosphorus-doped carbon material; wherein the temperature of the fast pyrolysis is controlled to be 350-1000 ℃, and the preferred temperature of the fast pyrolysis is 450-800 ℃; in the process, deep carbonization of acid hydrothermal products is realized, hierarchical pores are formed, and phosphorus is doped into a carbon skeleton.|[0056] The invention provides a method for converting agriculture and forestry biomass waste into a phosphorus-doped hierarchical porous carbon material by utilizing a phosphoric acid hydrothermal pretreatment combined fast pyrolysis technology, wherein the process is characterized in that the hydrothermal method and the fast pyrolysis method are not simply superposed, but acid, hydrothermal and fast pyrolysis are mutually coupled, so that a remarkable synergistic effect is achieved;|[0057] firstly, alkali metal and alkaline earth metal are main components of biomass ash, oxides of the biomass ash can be dissolved in acid solution, and related researches prove that the acid washing can achieve a relatively ideal deliming effect; the hot-pressing shrinkage in the hydrothermal pretreatment is water in a subcritical or supercritical state at the temperature of more than 100 ℃, the dielectric constant is reduced to be only 25-35, and is close to that of most organic solvents in a standard state, so that the deashing and carbonization reaction of biomass can be favorably carried out;|[0058] in addition, in the hydrothermal process of phosphoric acid, the phosphoric acid can enhance the hydrolysis reaction of biomasses such as hemicellulose, cellulose and the like in the hydrothermal reaction, so that the biomasses are changed into a loose and porous three-dimensional network structure, the permeation and dispersion of the phosphoric acid in the biomasses are facilitated, the acid in the solution can be effectively adsorbed, and the efficient and uniform loading of the acid is realized; the hydrothermal pre-carbonization can form a plurality of oxygen-containing functional groups on the organic material, and the biomass material can be changed into a loose and porous three-dimensional structure by using phosphoric acid, so that a large number of oxygen-containing functional groups can be formed on the surface and the loose internal three-dimensional structure of the material in the hydrothermal pre-treatment process of the phosphoric acid, the oxygen-containing functional groups can react with the phosphoric acid again, phosphate radicals are successfully loaded on the material, and the loading capacity is considerable, but the loading in the form does not really dope the P element into a carbon skeleton and further needs to be carbonized and activated;|[0059] because a loose structure is formed by phosphoric acid hydrothermal pre-carbonization, and a large amount of phosphate radicals are loaded, the material structure can be damaged by long-time high-temperature carbonization and activation operation, so that the carbon skeleton collapses, the final pore structure of the material is influenced, and on the other hand, the loaded P falls off, and the aim of forming an effective P-doped carbon material cannot be achieved; the fast pyrolysis usually adopts high-temperature gas to rapidly process biomass, the processing effect on blocky or glume materials is not good, the main target product of the fast pyrolysis technology is bio-oil, and the carbon yield after the processing is very low;|[0060] combine the hydrothermal method and the quick pyrolysis method two can make good use of the advantages and avoid the weak point, can carry out quick carbomorphism activation to the material inside of the loose structure who forms, make oxygen-containing functional group get rid of and form pore structure, a large amount of load P can obtain the chance of inserting the carbon skeleton here simultaneously, and the quick processing of short time has guaranteed again that the structure can not destroyed to reach final effect.|[0061] The invention selects the scheme of fast pyrolysis to combine with the phosphoric acid hydrothermal pre-carbonization, thus achieving very ideal effect only by fast pyrolysis in a very short time, greatly improving the carbon production efficiency and simultaneously obviously reducing the energy consumption; meanwhile, the existence of phosphorus can play a good role in carbon fixation, so that the carbon yield is improved;|[0062] in addition, the process method of phosphoric acid hydrothermal combined fast pyrolysis can overcome the problems of limited specific surface area, large ash content, low and uneven heteroatom doping amount, low carbon yield and the like of the activated carbon prepared by the traditional method; and the phosphorus not doped into the activated carbon can be recycled by washing, no phosphoric acid is discharged in the whole preparation process, the method has obvious advantages in the aspects of energy and environment, the whole process is green, simple and efficient, the raw material source is wide, and the method can be used for large-scale production.|INVENTION MODE|[0063] Example 1|[0064] In the embodiment, six different types of biomass raw materials are selected and crushed into particles of 40-80 meshes, 4g of the biomass particles are respectively weighed for standby, and the hierarchical porous phosphorus doped carbon material is respectively prepared according to the following preparation method;|[0065] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0066] crushing biomass into particles of 40-80 meshes;|[0067] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0068] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and carrying out hydrothermal reaction for 12 hours at the hydrothermal temperature of 200 ℃ to generate hydrothermal carbon;|[0069] step four, opening the reaction kettle after the reaction kettle is completely cooled, pouring hydrothermal carbon obtained after hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0070] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0071] Different rapidly pyrolyzed hierarchical-pore phosphorus-doped carbon materials are respectively collected and detected, and the specific surface areas of the phosphorus-doped carbon materials prepared from six different types of biomass are shown in table 1:|[0072] TABLE 1 specific surface area and elemental composition for the preparation of phosphorus-doped carbon materials from different biomass feedstocks|[0073] |INVENTION MODE|[0074] Example 2|[0075] In this example, the influence of different phosphorus sources and acid sources on the properties of the hierarchical porous phosphorus-doped carbon material was tested, only the types of the phosphorus sources and acid sources were changed, and the material was prepared according to the following preparation method;|[0076] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0077] crushing wood chip biomass into particles of 40-80 meshes;|[0078] step two, weighing 4g of crushed biomass particles and a phosphorus-containing acidic solution according to a phosphorus-carbon mass ratio of 3:1 to form a mixture;|[0079] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and carrying out hydrothermal reaction for 12 hours at the hydrothermal temperature of 200 ℃ to generate hydrothermal carbon;|[0080] step four, opening the reaction kettle after the reaction kettle is completely cooled, pouring hydrothermal carbon obtained after hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0081] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0082] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared by biomass under different phosphorus sources and acid sources are shown in table 2:|[0083] TABLE 2 specific surface area and elemental composition for the preparation of phosphorus-doped carbon materials from different phosphorus and acid sources|[0084] |INVENTION MODE|[0085] Example 3|[0086] In this example, the effect of different hydrothermal temperatures on the properties of the hierarchical pore phosphorus doped carbon material was tested, only the hydrothermal temperature was changed, and the material was prepared according to the following preparation method;|[0087] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0088] crushing wood chip biomass into particles of 40-80 meshes;|[0089] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0090] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and performing hydrothermal reaction for 12 hours at the hydrothermal temperatures of 70 ℃, 150 ℃, 200 ℃ and 300 ℃ respectively to generate hydrothermal carbon;|[0091] step four, opening the reaction kettle after the reaction kettle is completely cooled, pouring hydrothermal carbon obtained after hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0092] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0093] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared from biomass under the conditions of different hydrothermal temperatures are shown in table 3:|[0094] TABLE 3 specific surface area and elemental composition for preparation of phosphorus doped carbon materials at different hydrothermal temperatures|[0095] |[0096] |INVENTION MODE|[0097] Example 4|[0098] In this example, the effect of different hydrothermal times on the properties of the hierarchical pore phosphorus doped carbon material was tested, only the hydrothermal reaction time was changed, and the material was prepared according to the following preparation method;|[0099] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0100] crushing wood chip biomass into particles of 40-80 meshes;|[0101] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0102] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and performing hydrothermal reactions for 1h, 6h, 12h and 24h at 200 ℃ to generate hydrothermal carbon;|[0103] step four, opening the reaction kettle after the reaction kettle is completely cooled, pouring hydrothermal carbon obtained after hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0104] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0105] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared from biomass under the conditions of different hydrothermal reaction times are shown in table 4:|[0106] TABLE 4 specific surface area and elemental composition for preparation of phosphorus doped carbon materials at different hydrothermal reaction times|[0107] |[0108] |INVENTION MODE|[0109] Example 5|[0110] In this example, the effect of different phosphorus-carbon ratios on the properties of the hierarchical pore phosphorus-doped carbon material was tested, only the phosphorus-carbon ratio was changed, and the material was prepared according to the following preparation method;|[0111] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0112] crushing wood chip biomass into particles of 40-80 meshes;|[0113] step two, weighing 4g of crushed biomass particles, and uniformly mixing with a phosphoric acid solution according to the mass ratio of phosphorus to carbon of 0.1:1, 1:1, 2:1, 3:1, 4:1 and 5:1 to form a mixture;|[0114] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and carrying out hydrothermal reaction for 12 hours at the temperature of 200 ℃ to generate hydrothermal carbon;|[0115] pouring the hydrothermal carbon obtained after the hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0116] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0117] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared by biomass under the conditions of different phosphorus-carbon ratios are shown in table 2:|[0118] TABLE 5 specific surface area and elemental composition for preparation of phosphorus-doped carbon materials with different phosphorus to carbon ratios|[0119] |[0120] |INVENTION MODE|[0121] Example 6|[0122] In this example, the effect of different pyrolysis temperatures on the properties of a hierarchical pore phosphorus doped carbon material was tested, only the pyrolysis temperature was changed, and the material was prepared according to the following preparation method;|[0123] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0124] crushing wood chip biomass into particles of 40-80 meshes;|[0125] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0126] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and carrying out hydrothermal reaction for 12 hours at the temperature of 200 ℃ to generate hydrothermal carbon;|[0127] pouring the hydrothermal carbon obtained after the hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0128] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 350 ℃, 450 ℃, 700 ℃, 800 ℃ and 1000 ℃, controlling the time of fast pyrolysis for 5min, and performing fast cooling and collection to obtain the fast pyrolyzed multi-level-pore phosphorus-doped carbon material.|[0129] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared by biomass under different pyrolysis temperature conditions are shown in table 6:|[0130] TABLE 6 specific surface area and elemental composition for preparing phosphorus-doped carbon materials at different pyrolysis temperatures|[0131] |[0132] Comparative example 1|[0133] In this comparative example, the effect on the properties of a phosphorus-doped biomass carbon material was tested using only a hydrothermal reaction process of biomass with a phosphorus-containing acidic solution, i.e., without a fast pyrolysis method, and a phosphorus-doped carbon material was prepared according to the following preparation method;|[0134] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0135] crushing wood chip biomass into particles of 40-80 meshes;|[0136] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0137] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and performing hydrothermal reaction for 12 hours at 200 ℃ to generate hydrothermal carbon;|[0138] and step four, opening the reaction kettle after the reaction kettle is completely cooled, and pouring the hydrothermal carbon obtained after the hydrothermal reaction into a beaker for dehydration and drying to obtain the hydrothermal carbon.|[0139] Collecting the biomass source phosphorus-doped carbon material, detecting, and preparing the phosphorus-doped carbon material with the specific surface area of 537.3m2/g under the condition of not carrying out fast pyrolysis; comparing the data with the data of the embodiment 4, namely under the same conditions, the specific surface area of the phosphorus-doped carbon material subjected to the fast pyrolysis reaction is up to 2372.4m 2/g; thus, it is apparent that the parameters of the phosphorus doped carbon material produced using the present application are much better than the phosphorus doped carbon material produced by the comparative example method.|[0140] The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the present invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. (CN112010302)|TECHNICAL FIELD|[0002] The invention belongs to the field of preparation of phosphorus-doped carbon materials, and particularly relates to the field of preparation of a hierarchical porous phosphorus-doped carbon material by using biomass.|BACKGROUND ART|[0004] Biomass is the world's fourth largest energy source second only to coal, oil and gas, accounting for approximately 14% of the world's primary energy consumption. China produces approximately 24 million tons of waste biomass (crop straw, wood chips, weeds, etc.) per year. The energy sources stored in the waste biomasses are equivalent to 10 hundred million tons of standard coal, and the waste biomasses are a huge resource treasury. However, due to high labor cost, low economic benefit and increasingly strict environmental regulations, the recycling of the biomass is not widely promoted at present, and most of the biomass is directly discarded; the carbon material has the characteristics of good surface chemical property, excellent mechanical stability, rich pore channels, excellent conductivity and the like, and shows great advantages and potentials in the aspects of catalysis, hydrogen storage, separation and adsorption, electrochemistry and the like. Under the conditions of current resource shortage, gradual energy exhaustion and environmental deterioration, biomass wastes (such as various straws, chaffs, wood chips and the like) rich in resources are used as raw materials to prepare activated carbon, namely biomass-based activated carbon, which is considered to be one of the most effective modes for utilizing waste biomass; in recent years, in order to further improve the application of carbon materials in catalysis, adsorption, sensing, electrochemistry and the like, the achievement of unique performance of carbon materials through surface and structure modification is one of the research hotspots in recent years, and many scholars have increased research on phosphorus-doped carbon materials, compared with pure carbon materials, phosphorus-containing carbon materials contain hydrophilic acid surfaces and chemical stability, show high adsorption capacity on basic metal ions and organic molecules, and have good catalytic activity in various reactions.|[0005] Currently, methods for introducing phosphorus into carbon structures can be divided into three major categories:|[0006] (1) carrying out heat treatment after physically mixing or chemically bonding the carbon-containing precursor and the phosphorus-containing compound: the method is characterized in that a carbon-containing precursor and a phosphorus-containing compound are mixed and then carbonized, or the carbon-containing precursor and the phosphorus-containing compound are reacted to obtain a phosphorus-containing organic substance and then carbonized, and phosphorus atoms are introduced into a carbon skeleton in the carbonization process. This method is simple in process, but generally costly using an organic carbon precursor and a phosphorus-containing ligand.|[0007] (2) Post-treatment doping method: the method generally refers to introducing a functional group containing phosphorus atoms into an activated carbon material through surface modification such as a dry method or a wet method, and the like, and the method may cause structural collapse of the activated carbon material, so that the specific surface area of the activated carbon material is reduced, and the activated carbon material is difficult to uniformly dope the phosphorus atoms due to stable chemical properties.|[0008] (3) Vapor deposition of carbon and phosphorus: the method refers to the phosphorus-containing carbon prepared by forming solid substances deposited on a substrate through gas-phase chemical reaction between gaseous carbon-containing and phosphorus-containing compounds at medium temperature or high temperature, and the chemical reaction can be promoted by adopting plasma and laser auxiliary technology, so that the deposition can be carried out at lower temperature. The method has high requirements on equipment, high price, high technical requirements and difficult operation.|[0009] In recent years, some inventions have disclosed methods for producing phosphorus-doped carbon materials, but these methods are clearly different from the present invention. Such as the following prior patents:|[0010] a) CN 201710764307.2A preparation method and application of a phosphorus-doped biomass graded porous carbon material, the patent relates to the preparation of a phosphorus-doped biomass graded porous carbon material, and the preparation method comprises the following steps: the dried biomass is first crushed and then soaked in phytate solution for several hours. And then carrying out constant-temperature heat treatment for 1-10 h at 500-1000 ℃ under the protection of inert gas. Performing acid cooking and water cooking to remove impurities, and drying to obtain a phosphorus-doped biomass graded porous carbon material with the specific surface area of 800-2100 cm 2/g; the preparation method related in the patent is a one-step high-temperature direct carbonization method, is different from the method of combining hydrothermal pretreatment and fast pyrolysis of phosphoric acid in the patent, takes phosphorus-containing organic salt substances as a template agent, a phosphorus doping agent and a pore-forming agent, and is different from the phosphoric acid solution used in the patent. The phosphoric acid hydrothermal method has a certain phosphorus doping effect, and simultaneously has the effects of catalyzing biomass hydrolysis, carbonization, pore forming, ash removal and the like, so that the preparation of a high-performance carbon material is facilitated; although the multi-level pore material can be obtained by the patent, the pyrolysis time is longer, and the phosphorus doping amount is lower.|[0011] b) CN 201710171948.7A phosphorus doped mesoporous carbon material and a microwave preparation method thereof, the patent relates to a preparation method of the phosphorus doped mesoporous carbon material, the preparation method comprises the following steps: putting 6-10 g of phytic acid into an open quartz reactor, and then putting the quartz reactor into a microwave oven; heating for 1-5 minutes under an atmospheric atmosphere at the microwave power of 400-800W to obtain a black foam carbonization product; then soaking the carbonized product in 100mL of acid liquor with the mass percentage concentration of 1-4% for 1-4 hours at room temperature; filtering the soaking solution, and filtering and washing the solid with clear water until the pH value of the filtrate is neutral to obtain black powdery solid; drying the black powdery solid for 8-12 hours at the temperature of 80-120 ℃ to obtain the phosphorus-doped mesoporous carbon material; the preparation method directly takes the phosphorus-rich organic matter phytic acid as a precursor, but not biomass wastes, has higher cost and limited phosphorus doping rate, is a microwave carbonization method, and is different from the method combining hydrothermal pretreatment and fast pyrolysis of phosphoric acid;|[0012] c) CN 201810591723.1A phosphorus-doped microporous/mesoporous carbon material and a preparation method thereof, the patent relates to a preparation method of the phosphorus-doped microporous/mesoporous carbon material, the preparation method of the microporous/mesoporous carbon material comprises the following steps of cleaning okra with clear water, drying, and freeze-drying at-45 to-80 ℃ for 48 to 96 hours to obtain freeze-dried okra; then carrying out heat treatment for 2-4 hours at 700-900 ℃ to obtain a phosphorus-doped microporous/mesoporous carbon material; the pretreatment method related in the patent is low-temperature freeze-drying okra, is different from the acid hydrothermal pretreatment method in the patent, cannot realize synchronous deashing, acid loading and pre-carbonization, cannot promote the carbonization process and shorten the treatment time; the used raw materials are okra which can be used, but biomass waste is not used, so that the cost is high; the heat treatment is carried out for 2 to 4 hours at high temperature, the time consumption is long, the energy consumption is large, and the specific surface area of the prepared carbon material is small.|DISCLOSURE|[0013] Disclosure of Invention|[0014] In order to solve the problems, the invention achieves the purposes through the following technical scheme:|[0015] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0016] crushing biomass into tiny particles;|[0017] step two, uniformly mixing the crushed biomass particles and the phosphorus-containing acidic solution in proportion to form a mixture;|[0018] step three, placing the mixture into a hydrothermal reaction kettle, and carrying out hydrothermal reaction at a certain temperature to generate hydrothermal carbon;|[0019] step four, dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction;|[0020] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, and performing fast pyrolysis under the protection of inert atmosphere to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0021] As a further optimized scheme of the invention, in the first step, the biomass is any one or a combination of more than two of lignocellulose biomass, agricultural solid waste and municipal solid waste; the lignocellulose biomass comprises cellulose, lignin, xylose, xylan, glucose, cellobiose, starch, hemicellulose, chitosan, chitin, sucrose and fructose; coconut shell, olive kernel, apricot kernel, date kernel, peach kernel, almond shell, pecan shell, peanut shell, corn cob, Muricius seed, fruit pulp, wood, bagasse, moso bamboo, corn stalk, cotton stalk, hemp, rice hull, jackfruit peel, coffee grounds, smooth cord grass, bagasse, artichoke leaf, reed leaf, lotus stem, water hyacinth, hay, microalgae; the agricultural solid waste comprises rapeseed cakes, jatropha curcas cakes, cake pulp, vinasse, waste protein and animal waste, and the urban solid waste comprises waste paper, plastic waste and regenerated plastic.|[0022] As a further optimized scheme of the invention, the phosphorus-containing acidic solution in the second step is a phosphoric acid aqueous solution or an acidic phosphate solution.|[0023] As a further optimized scheme of the present invention, the acidic phosphate solution is any one of a solution formed by acidic phosphate and inorganic acid, a solution formed by acidic phosphate and organic acid, a solution formed by non-acidic phosphate and inorganic acid, and a solution formed by non-acidic phosphate and organic acid, the acidic phosphate includes dipotassium hydrogen phosphate, sodium dihydrogen phosphate, and ammonium dihydrogen phosphate, the non-acidic phosphate includes disodium hydrogen phosphate, sodium phosphate, potassium phosphate, calcium phosphate, and ammonium polyphosphate, the inorganic acid includes hydrochloric acid, sulfuric acid, phosphoric acid, and nitric acid, and the organic acid includes formic acid, acetic acid, citric acid, and oxalic acid.|[0024] As a further optimization scheme of the invention, the mixing ratio of the phosphorus-containing acidic solution and the biomass particles in the second step is controlled to be between 0.1:1 and 5:1 according to the phosphorus/carbon mass ratio.|[0025] As a further optimization scheme of the invention, the temperature of the hydrothermal reaction in the third step is 70-300 ℃.|[0026] As a further optimization scheme of the invention, the time of the hydrothermal reaction in the third step is 1-24 h.|[0027] As a further optimization scheme of the invention, the temperature of the fast pyrolysis in the fifth step is 350-1000 ℃.|[0028] As a further optimization scheme of the invention, the temperature of the fast pyrolysis in the fifth step is preferably 450-800 ℃.|[0029] As a further optimization scheme of the invention, the time for fast pyrolysis in the fifth step is 5 min.|[0030] The invention has the beneficial effects that:|[0031] 1) the invention selects the scheme of fast pyrolysis to combine with the phosphoric acid hydrothermal pre-carbonization, thus achieving very ideal effect only by fast pyrolysis in a very short time, greatly improving the carbon production efficiency and simultaneously obviously reducing the energy consumption; meanwhile, the existence of phosphorus can play a good role in carbon fixation, so that the carbon yield is improved;|[0032] 2) according to the invention, renewable biomass resources with wide sources are used as carbon sources, and the raw materials are clean and low in price;|[0033] 3) the phosphoric acid in the invention can be used as a phosphorus source to be doped into the carbon material and also can be used as an activating agent, so that synchronous pore-forming and phosphorus atom doping can be realized, and the doping amount is higher;|[0034] 4) the production process method is simple, convenient and feasible, short in time consumption and low in energy consumption, and is suitable for large-scale production.|DRAWINGS DESCRIPTION|[0036] FIG. 1 is an XPS spectrum of the phosphorus element of the phosphorus-doped carbon material of the present invention;|[0037] FIG. 2 is a nitrogen adsorption/desorption isotherm of a phosphorus-doped carbon material according to the present invention;|[0038] FIG. 3 is a TEM image of a phosphorus-doped carbon material according to the present invention;|[0039] FIG. 4 shows the results of nitrogen desorption tests of the phosphorus-doped carbon material of the present invention;|[0040] FIG. 5 is a flow chart of the steps of the manufacturing process of the present invention;|INVENTION MODE|[0041] Detailed Description|[0042] The present application will now be described in further detail with reference to the drawings, it should be noted that the following detailed description is given for illustrative purposes only and is not to be construed as limiting the scope of the present application, as those skilled in the art will be able to make numerous insubstantial modifications and adaptations to the present application based on the above disclosure.|[0043] A method for preparing a hierarchical porous phosphorus-doped carbon material from biomass as shown in fig. 1 to 5 comprises the following steps: the method comprises the following steps:|[0044] crushing biomass into tiny particles;|[0045] wherein, the biomass in the first step of the biomass is any one or the combination of more than two of lignocellulose biomass, agricultural solid waste and municipal solid waste; the lignocellulose biomass comprises cellulose, lignin, xylose, xylan, glucose, cellobiose, starch, hemicellulose, chitosan, chitin, sucrose and fructose; coconut shell, olive kernel, apricot kernel, date kernel, peach kernel, almond shell, pecan shell, peanut shell, corn cob, Muricius seed, fruit pulp, wood, bagasse, moso bamboo, corn stalk, cotton stalk, hemp, rice hull, jackfruit peel, coffee grounds, smooth cord grass, bagasse, artichoke leaf, reed leaf, lotus stem, water hyacinth, hay, microalgae; the agricultural solid waste comprises rapeseed cakes, jatropha curcas cakes, cake pulp, vinasse, waste protein and animal waste, and the urban solid waste comprises waste paper, plastic waste and regenerated plastic;|[0046] step two, mixing the crushed biomass particles with a phosphorus-containing acidic solution according to a phosphorus/carbon mass ratio of 0.1:1 to 5:1 to form a uniform mixture; in the process, the synergistic operation of biomass deliming, pore-forming, phosphoric acid loading and pre-carbonization is realized;|[0047] wherein the phosphorus-containing acidic solution is phosphoric acid aqueous solution or acidic phosphate solution,|[0048] the acidic phosphate solution is any one of a solution formed by acidic phosphate and inorganic acid, a solution formed by acidic phosphate and organic acid, a solution formed by non-acidic phosphate and inorganic acid and a solution formed by non-acidic phosphate and organic acid;|[0049] the acidic phosphate comprises dipotassium hydrogen phosphate, sodium dihydrogen phosphate, and ammonium dihydrogen phosphate;|[0050] the non-acidic phosphate comprises disodium hydrogen phosphate, sodium phosphate, potassium phosphate, calcium phosphate, and ammonium polyphosphate;|[0051] the inorganic acid comprises hydrochloric acid, sulfuric acid, phosphoric acid, and nitric acid;|[0052] the organic acid includes formic acid, acetic acid, citric acid, oxalic acid;|[0053] step three, placing the mixture into a hydrothermal reaction kettle, and controlling the temperature of the hydrothermal reaction to be 70-300 ℃ to carry out hydrothermal reaction to generate hydrothermal carbon; and the time of the hydrothermal reaction is 1h to 24 h;|[0054] step four, dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction;|[0055] putting the dried hydrothermal carbon into a pyrolysis furnace, and performing fast pyrolysis in the presence of inert atmosphere for 5min to obtain a fast pyrolyzed hierarchical porous phosphorus-doped carbon material; wherein the temperature of the fast pyrolysis is controlled to be 350-1000 ℃, and the preferred temperature of the fast pyrolysis is 450-800 ℃; in the process, deep carbonization of acid hydrothermal products is realized, hierarchical pores are formed, and phosphorus is doped into a carbon skeleton.|[0056] The invention provides a method for converting agriculture and forestry biomass waste into a phosphorus-doped hierarchical porous carbon material by utilizing a phosphoric acid hydrothermal pretreatment combined fast pyrolysis technology, wherein the process is characterized in that the hydrothermal method and the fast pyrolysis method are not simply superposed, but acid, hydrothermal and fast pyrolysis are mutually coupled, so that a remarkable synergistic effect is achieved;|[0057] firstly, alkali metal and alkaline earth metal are main components of biomass ash, oxides of the biomass ash can be dissolved in acid solution, and related researches prove that the acid washing can achieve a relatively ideal deliming effect; the hot-pressing shrinkage in the hydrothermal pretreatment is water in a subcritical or supercritical state at the temperature of more than 100 ℃, the dielectric constant is reduced to be only 25-35, and is close to that of most organic solvents in a standard state, so that the deashing and carbonization reaction of biomass can be favorably carried out;|[0058] in addition, in the hydrothermal process of phosphoric acid, the phosphoric acid can enhance the hydrolysis reaction of biomasses such as hemicellulose, cellulose and the like in the hydrothermal reaction, so that the biomasses are changed into a loose and porous three-dimensional network structure, the permeation and dispersion of the phosphoric acid in the biomasses are facilitated, the acid in the solution can be effectively adsorbed, and the efficient and uniform loading of the acid is realized; the hydrothermal pre-carbonization can form a plurality of oxygen-containing functional groups on the organic material, and the biomass material can be changed into a loose and porous three-dimensional structure by using phosphoric acid, so that a large number of oxygen-containing functional groups can be formed on the surface and the loose internal three-dimensional structure of the material in the hydrothermal pre-treatment process of the phosphoric acid, the oxygen-containing functional groups can react with the phosphoric acid again, phosphate radicals are successfully loaded on the material, and the loading capacity is considerable, but the loading in the form does not really dope the P element into a carbon skeleton and further needs to be carbonized and activated;|[0059] because a loose structure is formed by phosphoric acid hydrothermal pre-carbonization, and a large amount of phosphate radicals are loaded, the material structure can be damaged by long-time high-temperature carbonization and activation operation, so that the carbon skeleton collapses, the final pore structure of the material is influenced, and on the other hand, the loaded P falls off, and the aim of forming an effective P-doped carbon material cannot be achieved; the fast pyrolysis usually adopts high-temperature gas to rapidly process biomass, the processing effect on blocky or glume materials is not good, the main target product of the fast pyrolysis technology is bio-oil, and the carbon yield after the processing is very low;|[0060] combine the hydrothermal method and the quick pyrolysis method two can make good use of the advantages and avoid the weak point, can carry out quick carbomorphism activation to the material inside of the loose structure who forms, make oxygen-containing functional group get rid of and form pore structure, a large amount of load P can obtain the chance of inserting the carbon skeleton here simultaneously, and the quick processing of short time has guaranteed again that the structure can not destroyed to reach final effect.|[0061] The invention selects the scheme of fast pyrolysis to combine with the phosphoric acid hydrothermal pre-carbonization, thus achieving very ideal effect only by fast pyrolysis in a very short time, greatly improving the carbon production efficiency and simultaneously obviously reducing the energy consumption; meanwhile, the existence of phosphorus can play a good role in carbon fixation, so that the carbon yield is improved;|[0062] in addition, the process method of phosphoric acid hydrothermal combined fast pyrolysis can overcome the problems of limited specific surface area, large ash content, low and uneven heteroatom doping amount, low carbon yield and the like of the activated carbon prepared by the traditional method; and the phosphorus not doped into the activated carbon can be recycled by washing, no phosphoric acid is discharged in the whole preparation process, the method has obvious advantages in the aspects of energy and environment, the whole process is green, simple and efficient, the raw material source is wide, and the method can be used for large-scale production.|INVENTION MODE|[0063] Example 1|[0064] In the embodiment, six different types of biomass raw materials are selected and crushed into particles of 40-80 meshes, 4g of the biomass particles are respectively weighed for standby, and the hierarchical porous phosphorus doped carbon material is respectively prepared according to the following preparation method;|[0065] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0066] crushing biomass into particles of 40-80 meshes;|[0067] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0068] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and carrying out hydrothermal reaction for 12 hours at the hydrothermal temperature of 200 ℃ to generate hydrothermal carbon;|[0069] step four, opening the reaction kettle after the reaction kettle is completely cooled, pouring hydrothermal carbon obtained after hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0070] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0071] Different rapidly pyrolyzed hierarchical-pore phosphorus-doped carbon materials are respectively collected and detected, and the specific surface areas of the phosphorus-doped carbon materials prepared from six different types of biomass are shown in table 1:|[0072] TABLE 1 specific surface area and elemental composition for the preparation of phosphorus-doped carbon materials from different biomass feedstocks|[0073] |INVENTION MODE|[0074] Example 2|[0075] In this example, the influence of different phosphorus sources and acid sources on the properties of the hierarchical porous phosphorus-doped carbon material was tested, only the types of the phosphorus sources and acid sources were changed, and the material was prepared according to the following preparation method;|[0076] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0077] crushing wood chip biomass into particles of 40-80 meshes;|[0078] step two, weighing 4g of crushed biomass particles and a phosphorus-containing acidic solution according to a phosphorus-carbon mass ratio of 3:1 to form a mixture;|[0079] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and carrying out hydrothermal reaction for 12 hours at the hydrothermal temperature of 200 ℃ to generate hydrothermal carbon;|[0080] step four, opening the reaction kettle after the reaction kettle is completely cooled, pouring hydrothermal carbon obtained after hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0081] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0082] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared by biomass under different phosphorus sources and acid sources are shown in table 2:|[0083] TABLE 2 specific surface area and elemental composition for the preparation of phosphorus-doped carbon materials from different phosphorus and acid sources|[0084] |INVENTION MODE|[0085] Example 3|[0086] In this example, the effect of different hydrothermal temperatures on the properties of the hierarchical pore phosphorus doped carbon material was tested, only the hydrothermal temperature was changed, and the material was prepared according to the following preparation method;|[0087] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0088] crushing wood chip biomass into particles of 40-80 meshes;|[0089] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0090] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and performing hydrothermal reaction for 12 hours at the hydrothermal temperatures of 70 ℃, 150 ℃, 200 ℃ and 300 ℃ respectively to generate hydrothermal carbon;|[0091] step four, opening the reaction kettle after the reaction kettle is completely cooled, pouring hydrothermal carbon obtained after hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0092] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0093] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared from biomass under the conditions of different hydrothermal temperatures are shown in table 3:|[0094] TABLE 3 specific surface area and elemental composition for preparation of phosphorus doped carbon materials at different hydrothermal temperatures|[0095] |[0096] |INVENTION MODE|[0097] Example 4|[0098] In this example, the effect of different hydrothermal times on the properties of the hierarchical pore phosphorus doped carbon material was tested, only the hydrothermal reaction time was changed, and the material was prepared according to the following preparation method;|[0099] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0100] crushing wood chip biomass into particles of 40-80 meshes;|[0101] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0102] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and performing hydrothermal reactions for 1h, 6h, 12h and 24h at 200 ℃ to generate hydrothermal carbon;|[0103] step four, opening the reaction kettle after the reaction kettle is completely cooled, pouring hydrothermal carbon obtained after hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0104] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0105] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared from biomass under the conditions of different hydrothermal reaction times are shown in table 4:|[0106] TABLE 4 specific surface area and elemental composition for preparation of phosphorus doped carbon materials at different hydrothermal reaction times|[0107] |[0108] |INVENTION MODE|[0109] Example 5|[0110] In this example, the effect of different phosphorus-carbon ratios on the properties of the hierarchical pore phosphorus-doped carbon material was tested, only the phosphorus-carbon ratio was changed, and the material was prepared according to the following preparation method;|[0111] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0112] crushing wood chip biomass into particles of 40-80 meshes;|[0113] step two, weighing 4g of crushed biomass particles, and uniformly mixing with a phosphoric acid solution according to the mass ratio of phosphorus to carbon of 0.1:1, 1:1, 2:1, 3:1, 4:1 and 5:1 to form a mixture;|[0114] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and carrying out hydrothermal reaction for 12 hours at the temperature of 200 ℃ to generate hydrothermal carbon;|[0115] pouring the hydrothermal carbon obtained after the hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0116] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 450 ℃, controlling the time of the fast pyrolysis at 5min, and performing fast cooling and collection to obtain the fast pyrolyzed hierarchical porous phosphorus-doped carbon material.|[0117] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared by biomass under the conditions of different phosphorus-carbon ratios are shown in table 2:|[0118] TABLE 5 specific surface area and elemental composition for preparation of phosphorus-doped carbon materials with different phosphorus to carbon ratios|[0119] |[0120] |INVENTION MODE|[0121] Example 6|[0122] In this example, the effect of different pyrolysis temperatures on the properties of a hierarchical pore phosphorus doped carbon material was tested, only the pyrolysis temperature was changed, and the material was prepared according to the following preparation method;|[0123] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0124] crushing wood chip biomass into particles of 40-80 meshes;|[0125] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0126] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and carrying out hydrothermal reaction for 12 hours at the temperature of 200 ℃ to generate hydrothermal carbon;|[0127] pouring the hydrothermal carbon obtained after the hydrothermal reaction into a beaker for dehydration and drying to obtain phosphoric acid hydrothermal carbon;|[0128] and fifthly, putting the dried hydrothermal carbon into a pyrolysis furnace, performing fast pyrolysis under the protection of inert atmosphere, controlling the temperature of the fast pyrolysis furnace at 350 ℃, 450 ℃, 700 ℃, 800 ℃ and 1000 ℃, controlling the time of fast pyrolysis for 5min, and performing fast cooling and collection to obtain the fast pyrolyzed multi-level-pore phosphorus-doped carbon material.|[0129] Collecting different rapidly pyrolyzed hierarchical porous phosphorus-doped carbon materials and detecting, wherein the specific surface areas of the hierarchical porous phosphorus-doped carbon materials prepared by biomass under different pyrolysis temperature conditions are shown in table 6:|[0130] TABLE 6 specific surface area and elemental composition for preparing phosphorus-doped carbon materials at different pyrolysis temperatures|[0131] |[0132] Comparative example 1|[0133] In this comparative example, the effect on the properties of a phosphorus-doped biomass carbon material was tested using only a hydrothermal reaction process of biomass with a phosphorus-containing acidic solution, i.e., without a fast pyrolysis method, and a phosphorus-doped carbon material was prepared according to the following preparation method;|[0134] a method for preparing a hierarchical porous phosphorus-doped carbon material from biomass comprises the following steps:|[0135] crushing wood chip biomass into particles of 40-80 meshes;|[0136] step two, weighing 4g of crushed biomass particles and phosphoric acid solution according to the mass ratio of phosphorus to carbon of 3:1 to form a mixture;|[0137] step three, putting the mixture into a 50ml hydrothermal reaction kettle, and performing hydrothermal reaction for 12 hours at 200 ℃ to generate hydrothermal carbon;|[0138] and step four, opening the reaction kettle after the reaction kettle is completely cooled, and pouring the hydrothermal carbon obtained after the hydrothermal reaction into a beaker for dehydration and drying to obtain the hydrothermal carbon.|[0139] Collecting the biomass source phosphorus-doped carbon material, detecting, and preparing the phosphorus-doped carbon material with the specific surface area of 537.3m2/g under the condition of not carrying out fast pyrolysis; comparing the data with the data of the embodiment 4, namely under the same conditions, the specific surface area of the phosphorus-doped carbon material subjected to the fast pyrolysis reaction is up to 2372.4m 2/g; thus, it is apparent that the parameters of the phosphorus doped carbon material produced using the present application are much better than the phosphorus doped carbon material produced by the comparative example method.|[0140] The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the present invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Family Number|(91712277)|91712277|Abstract|(CN112010302 A)|The invention relates to a method for preparing a hierarchical - pore phosphorus - doped carbon material from biomass . The method comprises the following steps : firstly , crushing the biomass into tiny particles ; then uniformly mixing the crushed biomass particles with a phosphoric acid - containing solution according to a certain ratio to form a mixture ; putting the mixture into a hydrothermal reactionkettle , and carrying out a hydrothermal reaction at a certain temperature to generate hydrothermal carbon ; dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction ; andputting the dried hydrothermal carbon into a pyrolyzing furnace , and carrying out rapid pyrolysis under the protection of an inert atmosphere to obtain a hierarchical - pore phosphorus - doped carbon material after rapid pyrolysis . According to the method disclosed by the invention , a rapid pyrolysis scheme is combined with phosphoric acid hydrothermal pre - carbonization , so a very ideal effect can beachieved only by performing rapid pyrolysis in a very short time , carbon preparation efficiency is greatly improved , and energy consumption is remarkably reduced ; and meanwhile , due to the existence of phosphorus , a good carbon sequestration effect can be achieved , and carbon yield is increased . |CPC codes|(CN112010302 A)|C01B - 032/324 |C01B - 032/342 |IPC codes|(CN112010302 A)|C01B - 032/324 |C01B - 032/342 | Materials, metallurgy C01B-032/324|C01B-032/342|Y02P-020/10 C01B-032/324|C01B-032/342|Y02P-020/10 C01B-032/324|C01B-032/342 C01B-032/324|C01B-032/342 CN116812909|CN120348923|CN118754121|CN113387355|CN112194127|CN117567089|CN117548129|CN117208887|CN116618018|CN114392719|CN112777583|CN111362251|US12371328|CN118289752B|CN116218557B|CN114141986B CN116812909 106686174 WHO=Examiner SELF=N CAT=Y CAT=X|CN120348923 115377532 WHO=Examiner SELF=N CAT=Y|CN118754121 111734240 WHO=Examiner SELF=N CAT=X|CN113387355 96060393 WHO=Examiner SELF=Y CAT=X|CN112194127 92250385 WHO=Examiner SELF=Y CAT=X|CN117567089 108572885 WHO=Examiner SELF=Y CAT=A|CN117548129 108513151 WHO=Examiner SELF=N CAT=A|CN117208887 107698950 WHO=Examiner SELF=N CAT=A|CN116618018 106195752 WHO=Examiner SELF=N CAT=A|CN114392719 99765623 WHO=Examiner SELF=Y CAT=A|CN112777583 93984437 WHO=Examiner SELF=N CAT=A|CN111362251 89549348 WHO=Examiner SELF=N CAT=A|US12371328 110494461 WHO=Applicant SELF=N|CN118289752B 110494461 WHO=Examiner SELF=N|CN116218557B 105224576 WHO=Examiner SELF=N|CN114141986B 98981732 WHO=Examiner SELF=N CN109354015|CN110176602|WO201899173|CN108529587|CN106115652 CN109354015 83444951 WHO=Examiner SELF=Y CAT=X|CN110176602 85807664 WHO=Examiner SELF=N CAT=A|WO201899173 79963230 WHO=Examiner SELF=N CAT=A|CN108529587 81310470 WHO=Examiner SELF=N CAT=A|CN106115652 74593971 WHO=Examiner SELF=N CAT=A 邢献军等: &quot;磷掺杂葵花盘基活性炭在锂离子电池负极材料中的应用&quot;, 《过程工程学报》 (Cat. A)|任芝军: &quot;《固体废弃物处理外置与资源化技术》&quot;, 31 May 2010, 哈尔滨工业大学出版社 (Cat. A) CN106115652; WO201899173; CN108529587; CN109354015; CN110176602 REVOKED (CN112010302)|REVOKED DEAD (CN112010302)|DEAD (CN112010302)|LEGAL DETAILS FOR CN112010302|Actual or expected expiration date=2022-12-23|Legal state=DEAD|Status=REVOKED|Event publication date=2020-09-07|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202010926200|Application date=2020-09-07|Standardized application number=2020CN-0926200|Event publication date=2020-12-01|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN112010302|Publication stage code=A|Publication date=2020-12-01|Standardized publication number=CN112010302|Event publication date=2020-12-01|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2020-12-18|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2022-12-23|Event code=CN/RJ01|Event indicator=Neg|Event group=Event indicating Not In Force|Rejection of an application after its publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQ8MYjBF0JCo1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000054875185&ekey=2169&xpn=CN112010302&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=mruGvYRlPqufANnoTk4A3ZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN112010302)|CN (CN112010302)|NAME=HEFEI UNIVERSITY OF TECHNOLOGY , COUNTRY=CN (CN112010302)|NAME=HONG LING;HEFEI ZHONGGU INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=34146 (CN112010302)|NAME=MA PEIYONG|NAME=LIN FENGFEI|NAME=ZHANG YING|NAME=LIU XIAOHAO|NAME=HUANG RUIYI|NAME=QI FENGLEI|NAME=XING XIANJUN 0 1 Titre: (CN112010302)|Method for preparing hierarchical-pore phosphorus-doped carbon material from biomass Résumé: (CN112010302)|The invention relates to a method for preparing a hierarchical-pore phosphorus-doped carbon material from biomass. The method comprises the following steps: firstly, crushing the biomass into tiny particles; then uniformly mixing the crushed biomass particles with a phosphoric acid-containing solution according to a certain ratio to form a mixture; putting the mixture into a hydrothermal reactionkettle, and carrying out a hydrothermal reaction at a certain temperature to generate hydrothermal carbon; dehydrating and drying the hydrothermal carbon obtained after the hydrothermal reaction; andputting the dried hydrothermal carbon into a pyrolyzing furnace, and carrying out rapid pyrolysis under the protection of an inert atmosphere to obtain a hierarchical-pore phosphorus-doped carbon material after rapid pyrolysis. According to the method disclosed by the invention, a rapid pyrolysis scheme is combined with phosphoric acid hydrothermal pre-carbonization, so a very ideal effect can beachieved only by performing rapid pyrolysis in a very short time, carbon preparation efficiency is greatly improved, and energy consumption is remarkably reduced; and meanwhile, due to the existence of phosphorus, a good carbon sequestration effect can be achieved, and carbon yield is increased. 107 Abstract gpt-4o-mini no The article focuses on preparing a carbon material from biomass and does not involve the accelerated weathering of minerals or CO₂ capture through mineral carbonation.
108 US63/497,890|US63/497,890P|US18/645,286|WOUS2024/026093 WOUS2024/026093|IN202517114935|EP24797870|KR10-2025-7039321|CN202480034823|AU2024264529|US18/645,286 EP4705006|CN121605002|KR10-2026-0027884|IN202517114935|AU2024264529|WO2024/226673|WO2024/226673|US20240350972 115038942 WO2024/226673 A3 2025-01-09 [WO2024226673]|WO2024/226673 A2 2024-10-31 [WO2024226673]|IN202517114935 A 2025-12-19 [IN202517114935]|EP4705006 A2 2026-03-11 [EP4705006]|KR10-2026-0027884 A 2026-03-03 [KR20260027884]|CN121605002 A 2026-03-03 [CN121605002]|AU2024264529 A1 2025-11-06 [AU2024264529]|US20240350972 A1 2024-10-24 [US20240350972] 2023-04-24|2024-04-24 2024-04-24|2025-11-21|2024-04-24|2024-04-24|2024-04-24|2024-04-24|2024-04-24 2026-03-11|2026-03-03|2026-03-03|2025-12-19|2025-11-06|2025-01-09|2024-10-31|2024-10-24 (EP4705006)|2044-04-24|(US20240350972)|2044-04-24|(WO2024/226673)|2026-10-24|(CN121605002)|2044-04-24|(KR10-2026-0027884)|2044-04-24|(IN202517114935)|2044-04-24|(AU2024264529)|2044-04-24 (EP4705006)|Ship based carbon capture, systems and methods of use thereof (EP4705006)|Many embodiments are directed to reactors and methods for reducing ship exhaust polluting emissions. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) for carbon dioxide sequestration. Certain embodiments may also be used to mitigate high acidity of SOx scrubber effluents, while some embodiments solve both issues (i.e., seawater acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely and permanently stored in the ocean. CALCAREA|KALKARIA (EP4705006)|Calcarea, Inc. ([US])|(US20240350972)|Calcarea, Inc. ([US])|(WO2024/226673)|CALCAREA, INC. ([US])|(WO2024/226673)|CALCAREA, INC. ([US])|(CN121605002)|Kalkaria Co.,Ltd. ([US])|(KR10-2026-0027884)|CALCAREA, INC. ([US])|(IN202517114935)|CALCAREA INC|(AU2024264529)|CALCAREA, INC. ADKINS JESS FIREY|FORIN PIERRE|GUTIERREZ MELISSA (EP4705006)|ADKINS, Jess, Firey|FORIN, Pierre|GUTIERREZ, Melissa (EP4705006)|Patentanwaltskanzlei Matschnig & Forsthuber OG;Biberstraße 22 ([AT])|Reg. Nb: 101506908|(WO2024/226673)|PECK, John, W. ([US])|(CN121605002)|ZHAO FANGXIAN;CCPIT PATENT AND TRADEMARK LAW OFFICE|Reg. Nb: 11038|(KR10-2026-0027884)|YOU ME PATENT & LAW FIRM|(AU2024264529)|Monks IP ([AU]) (US20240350972)|These and other features and advantages of the present invention will be better understood by reference to the following detailed description when considered in conjunction with the accompanying data and figures, wherein:|Thus, neutralizing the SOx effluent is important to avoid damage to sea life and/or infrastructure.| (US20240350972)|1. A reactor for integrating an AWL process with a SOx scrubbing process on a ship producing CO2 and SOx emissions, the reactor comprising: at least one chamber filled with a reaction medium, a water inlet in fluid communication with an aqueous effluent outlet of an absorber tower, a gas inlet in fluid communication with a gas effluent outlet of the absorber tower, an AWL effluent outlet, and any number of pumps, controls, and safety valves necessary for moving seawater and gas through the reactor at a desired rate.|10. A method for alleviating CO2 and SOx emissions pollution produced by a ship comprising: installing an AWL reactor aboard the ship, the AWL reactor comprising: at least one chamber filled with a reaction medium, a water inlet in fluid communication with an aqueous effluent outlet of a SOx scrubber aboard the ship, a gas inlet in fluid communication with a gas effluent outlet of the SOx scrubber, an AWL effluent outlet, and any number of pumps, controls, and safety valves necessary for moving seawater and gas through the AWL reactor at a desired rate; flowing seawater from the aqueous effluent outlet and a gas from the gas effluent outlet from the SOx scrubber into the AWL reactor; to mitigate the acidity of the seawater outflowing from the aqueous effluent outlet, while also safely storing carbon dioxide produced by the ship in the ocean.| (US20240350972)|The current disclosure is directed to methods of carbon dioxide sequestration, more specifically, to ship-based reactors capable of sequestering carbon dioxide and/or deacidifying SOx scrubber effluent.|This application is directed to embodiments of a reactor and a method for integrating an AWL process with a SOx scrubbing process on a ship producing CO2 and SOx emissions, such as to mitigate the acidity of the aqueous effluent of the SOx scrubbing process, while also safely storing carbon dioxide from the ship's exhaust in the ocean.| (US20240350972)|REACTOR(100,25)|SHIP(100,18)|SOX SCRUBBING(100,6)|SOX EMISSION(100,5)|INTEGRATING AWL(100,3)|SHIP PRODUCING CO2(100,3)|ALLEVIATING CO2(100,2)|CARBON CAPTURE(100,2)|SOX EMISSION POLLUTION(100,2)|DEACIDIFYING SOX SCRUBBER EFFLUENT(100,1)|SHIP CARBON CAPTURE(100,1)|SOX SCRUBBER(70,31)|MITIGATE ACIDITY(63,5)|AWL REACTOR(61,41)|AWL EFFLUENT OUTLET(61,5)|AQUEOUS EFFLUENT OUTLET(60,9)|ABSORBER TOWER(50,10)|GAS EFFLUENT OUTLET(44,6)|LIMESTONE ACCELERATED WEATHERING(43,2)|SOX EFFLUENT(42,1)|SEAWATER ACIDIFICATION(38,1)|SHIP REACTOR(36,1)|FLUID COMMUNICATION(32,10)|CARBON DIOXIDE SEQUESTRATION(31,2)|SEQUESTERING CO2(30,5)|MOVING SEAWATER(29,5)|REACTION MEDIUM(27,22)|SEA(24,9)|SHIP EXHAUST(24,4)|AQUEOUS EFFLUENT(21,9)|SEAWATER FLOW(21,6)|FINE GRAINED SOLID(20,5)|GAS INLET(20,5)|INFRASTRUCTURE(20,1)|SEAWATER(19,15)|WATER INLET(17,5)|CARBON DIOXIDE(16,16)|ARAGONITE(16,5)|SHIP REDUCTION(16,1)|OLIVINE(15,5)|PYROXENE(15,5)|VATERITE(15,5)|POLLUTING EMISSION(15,1)|AWL REACTOR CHAMBER(14,7)|CALCITE(14,5)|DOLOMITE(14,5)|MAFIC ROCK(14,5)|SILICATE(14,5)|CARBON DIOXIDE(14,2)|CARBON DIOXIDE POLLUTION(13,2)|SOX SCRUBBER EFFLUENT ACIDITY(13,1)|MGSIO(12,5)|NA2CO3(12,5)|SOX SCRUBBER AQUEOUS EFFLUENT(12,2)|SHIP SOX SCRUBBER EFFLUENT(12,1)|SAFETY VALVE(11,6)|NAHCO3(11,5)|REAGENT(11,5)|CARGO SHIP(11,2)|SEA LIFE(11,1)|CAO(10,5)|SEAWATER SOX SCRUBBER(10,1)|CONTAINER SHIP(8,3)|AWL REACTOR ABILITY(8,2)|SCRUBBER EFFLUENT WATER(8,2)|SHIP EXHAUST STACK(8,2)|ACCOMPANIMENT DATA(8,1)|ACIDIFIED EFFLUENT NEUTRALIZATION(8,1)|AWL REACTOR AWL CHAMBER(8,1)|AWL REACTOR EFFLUENT(8,1)|INCOMING CO2 INCOMPLETE TITRATION(8,1)|SCRUBBER ABSORBER TOWER(8,1)|SHIP EXHAUST CO2 CAPTURE(8,1)|UNDERWAY SEA CHEST(8,1)|AWL REACTOR PERFORMANCE(7,2)|ONBOARD SHIP(7,2)|PANAMAX CO2 EMISSION(7,1)|AWL REACTION MEDIUM(6,4)|BICARBONATE ION(6,4)|AWL EFFLUENT PH(6,1)|AWL OPTIMIZATION(6,1)|CO2 SEQUESTRATION NONLINEARITY(6,1)|SEAWATER ALKALINITY(6,1)|SOX ACIDITY(6,1)|SOX SCRUBBER GAS EFFLUENT(6,1)|BULK CARRIER(5,4)|CO2 NONLINEAR RESPONSE(5,2)|ABUNDANT BICARBONATE HCO3(5,1)|ANTHROPOGENIC CO2 GENERATION(5,1)|AWL REACTION PACKED BED(5,1)|AWL REACTOR EQUIPMENT(5,1)|CACO3 DISSOLUTION(5,1)|EFFLUENT WATER ACIDITY(5,1)|GENERAL TRADE(5,1)|HR BALLAST PUMP(5,1)|NONACIDIFIED SEAWATER SOURCE(5,1)|PANAMAX SHIP(5,1)|SEAWATER EFFLUENT(5,1)|SHIP CONSTRAINT(5,1)|SHIP EMITTED CO2(5,1)|SHIP WATERLINE(5,1)|SOX REACTOR(5,1)|PCO(4,5)|AMBIENT SEAWATER(4,1)|ANTHROPOGENIC CARBON PERMANENT STORAGE(4,1)|AWL FLUIDIZED BED REACTOR(4,1)|AWL REACTOR REACTION MEDIUM(4,1)|CO2 INTRODUCTION(4,1)|CO2 STREAM(4,1)|EARTH CO2(4,1)|ECONOMIC HEALTH(4,1)|EXHAUST HR(4,1)|EXTRA SEAWATER(4,1)|FUEL SULFUR(4,1)|GROWING CONCERN(4,1)|ONBOARD AWL PROCESS OPTIMIZATION(4,1)|PACKED BED CHAMBER(4,1)|REACTOR DIMENSION(4,1)|LIMESTONE SOLID(3,2)|SEAWATER FUNCTION(3,2)|TREND(3,2)|BUFFERING ABILITY(3,1)|CO2 PERMANENT STORAGE(3,1)|EARTH ATMOSPHERE(3,1)|EMISSION STREAM(3,1)|FUTURE RELEASE(3,1)|MULTISTAGE AWL REACTOR DESIGN(3,1)|NEUTRALIZING(3,1)|POTENT GREENHOUSE GAS(3,1)|SCRUBBER AQUEOUS EFFLUENT CAUSE(3,1)|SHIP AMBIENT WATER(3,1)|SOX SCRUBBING TOWER NUMBER(3,1)|SULFATE ION(3,1)|TOTAL SHIP EMISSION(3,1)|WORLDWIDE CARBON(3,1)||(WO2024/226673)|CARBON CAPTURE(100,1)|LIMESTONE ACCELERATED WEATHERING(100,1)|SHIP CARBON CAPTURE(100,1)|SOX SCRUBBER EFFLUENT(63,1)|ACCELERATED WEATHERING(62,1)|SEAWATER ACIDIFICATION(45,1)|MITIGATE ACIDITY(41,1)|CARBON DIOXIDE SEQUESTRATION(37,1)|REACTOR(33,2)|SHIP REDUCTION(31,1)|POLLUTING EMISSION(28,1)|AWL(21,1)|CARBON DIOXIDE POLLUTION(19,1)||(WO2024/226673)|CARBON CAPTURE(100,1)|LIMESTONE ACCELERATED WEATHERING(100,1)|SHIP CARBON CAPTURE(100,1)|SOX SCRUBBER EFFLUENT(63,1)|ACCELERATED WEATHERING(62,1)|SEAWATER ACIDIFICATION(45,1)|MITIGATE ACIDITY(41,1)|CARBON DIOXIDE SEQUESTRATION(37,1)|REACTOR(33,2)|SHIP REDUCTION(31,1)|POLLUTING EMISSION(28,1)|AWL(21,1)|CARBON DIOXIDE POLLUTION(19,1)||(CN121605002)|AWL REACTOR(100,43)|CARBON CAPTURE(100,3)|SHIP CARBON CAPTURE(100,1)|AQUEOUS EFFLUENT OUTLET(98,9)|AWL EFFLUENT OUTLET(94,5)|INTEGRATING AWL(93,3)|MITIGATE ACIDITY(89,3)|GAS EFFLUENT OUTLET(73,6)|ABSORBER AQUEOUS EFFLUENT OUTLET(68,2)|SEAWATER ACIDIFICATION(62,1)|SHIP REACTOR(59,1)|ABSORBER GAS EFFLUENT OUTLET(57,2)|FLUID COMMUNICATION(52,10)|SEAWATER(48,20)|VESSEL EXHAUST(47,1)|X SCRUBBER(46,43)|REACTOR(46,16)|X SCRUBBING(45,3)|LIMESTONE SOLID DISSOLUTION(45,2)|REACTION MEDIUM(44,21)|X EMISSION POLLUTION(44,2)|SEA(39,9)|X SCRUBBER EFFLUENT(39,3)|POLLUTION ABATEMENT(39,1)|SEQUESTERING CARBON DIOXIDE(37,1)|AQUEOUS EFFLUENT(36,14)|WATER RESOURCE ACIDIFICATION(36,1)|SEAWATER FLOW(35,5)|EXHAUST GAS POLLUTION EMISSION(35,1)|INFRASTRUCTURE(33,1)|NEUTRALIZING(33,1)|GAS INLET(32,5)|CARBON DIOXIDE SEQUESTRATION(32,3)|WATER INLET(29,5)|MARINE ORGANISM(29,1)|GAS ADSORPTION(28,2)|LIMESTONE SOLID(28,2)|ARAGONITE(26,5)|FINE GRAINED SOLID(26,2)|OLIVINE(24,5)|PYROXENE(24,5)|VATERITE(24,5)|X EFFLUENT(24,2)|URGENT NEED(24,1)|CALCITE(23,5)|DOLOMITE(23,5)|MAFIC ROCK(23,5)|AWL REACTOR CHAMBER(22,7)|CARBON DIOXIDE POLLUTION(22,2)|ATOMIZED SEAWATER MIST(21,2)|SHIP(20,8)|MGSIO(20,5)|NAHCO(20,5)|SILICATE(20,5)|SEAWATER SOURCE(19,3)|CARGO SHIP(19,2)|SAFETY VALVE(18,6)|CARBON DIOXIDE(16,10)|CAO(16,5)|CONTAINER SHIP(14,3)|CARBON DIOXIDE EMISSION(14,1)|WATER RESOURCE(14,1)|AWL REACTOR ABILITY(13,2)|SHIP EXHAUST STACK(13,2)|ACCOMPANIMENT DATA(13,1)|ACIDIFIED EFFLUENT NEUTRALIZATION(13,1)|AWL REACTOR AWL CHAMBER(13,1)|AWL REACTOR PERFORMANCE(12,2)|AWL REACTOR EFFLUENT(12,1)|X SCRUBBING(11,3)|AWL REACTION MEDIUM(10,4)|GASEOUS EFFLUENT(10,2)|FUEL SULFUR(9,2)|AWL EFFLUENT(9,1)|AWL OPTIMIZATION(9,1)|AWL REACTION PACKED BED(9,1)|BALLAST SEAWATER(9,1)|EFFLUENT ACIDITY(9,1)|SEAWATER ALKALINITY(9,1)|SEAWATER EFFLUENT(9,1)|SHIP CONFINES(9,1)|X SCRUBBER ABSORBER TOWER(9,1)|BULK CARRIER(8,4)|BALLAST PUMP(8,2)|INCOMPLETE TITRATION(8,1)|SENSITIVITY STEM(8,1)|EARTH ATMOSPHERE(7,2)|GAS EFFLUENT(7,2)|NONLINEAR RESPONSE(7,2)|NONLINEARITY(7,2)|BICARBONATE ION(6,5)|PCO(6,4)|AMBIENT SEAWATER(6,1)|AWL FLUIDIZED BED REACTOR(6,1)|AWL PH(6,1)|BOAT OPERATOR(6,1)|ECONOMIC HEALTH(6,1)|PACKED BED CHAMBER(6,1)|SHIP ENVIRONMENT(6,1)|SULFUR EXPORT(6,1)|TRAVELING SEA CHEST(6,1)|TREND(5,2)|ABSORBING GAS(5,1)|ARTIFICIAL CARBON PERMANENT STORAGE(5,1)|EXHAUST STREAM(5,1)|FUTURE RELEASE(5,1)|GREENHOUSE GAS POWER(5,1)|MULTISTAGE AWL REACTOR DESIGN(5,1)|NEUTRALIZING ACID(5,1)|SO X SCRUBBER EFFLUENT(5,1)|SULFURIC ACID PROTON(5,1)|TOTAL SHIP EMISSION(5,1)|WORLDWIDE CARBON(5,1)|FINELY DIVIDED SOLID(4,3)|BUFFERING CAPACITY BENEFIT(4,1)|CAPTURE CARBON DIOXIDE(4,1)||(KR10-2026-0027884)|SOX SCRUBBER(100,34)|CARBON CAPTURE(100,3)|SHIP CARBON CAPTURE(100,1)|SOX SCRUBBER EFFLUENT ACIDITY(98,2)|SOX SCRUBBER EFFLUENT(85,5)|AWL REACTOR(79,43)|SOX SCRUBBER GAS OUTLET(75,4)|INTEGRATING AWL(75,3)|SOX EMISSION POLLUTION(65,2)|ABSORPTION TOWER(58,8)|SEAWATER ACIDITY(56,2)|SEAWATER ACIDIFICATION(53,1)|AWL OUTLET(50,5)|SEQUESTERING CO2(49,2)|ABSORPTION TOWER GAS OUTLET(47,1)|MITIGATE ACIDITY(47,1)|SOX SCRUBBING(45,5)|SOX SCRUBBER WATER OUTLET(44,2)|FLUID COMMUNICATION(41,10)|VESSEL REACTOR(41,1)|WATER OUTLET(39,7)|SCRUBBER EFFLUENT(39,3)|SOX EMISSION(37,2)|VESSEL DISCHARGING(37,2)|GAS OUTLET(36,6)|REACTION MEDIUM(35,22)|SEAWATER(34,22)|SEA(32,8)|SEQUESTRATING CARBON DIOXIDE(32,1)|REDUCING POLLUTION EMISSION(31,1)|REACTOR(30,17)|AWL REACTOR CHAMBER(29,6)|WATER RESOURCE ACIDIFICATION(29,1)|PACKED BED(28,6)|SEAWATER FLOW(28,5)|VESSEL EXHAUST(28,1)|INFRASTRUCTURE(27,1)|POLLUTION REDUCTION SOLUTION(27,1)|GAS INLET(26,5)|AWL REACTION MEDIUM(24,3)|BULK SHIP(24,3)|LIMESTONE(22,9)|BATERITE(22,5)|SOX(21,8)|SHIP SOX SCRUBBER(21,3)|NAHCO(21,2)|ARAGONITE(20,5)|CARBON DIOXIDE SEQUESTRATION(20,2)|CARBON DIOXIDE POLLUTION(20,1)|URGENT NEED(20,1)|MAFIC ROCK(19,5)|OLIVINE(19,5)|PYROXENE(19,5)|CALCITE(18,5)|DOLOMITE(18,5)|BUFFERING CAPACITY(18,1)|MARINE LIFE(17,1)|FINE GRAINED SOLID(16,5)|MGSIO(16,5)|SILICATE(16,5)|AQUEOUS PHASE EFFLUENT(16,2)|CARGO SHIP(16,2)|SOX SCRUBBER AQUEOUS EFFLUENT(16,2)|SAFETY VALVE(15,6)|REAGENT(15,5)|WATER INLET(15,3)|DISCHARGE WATER(15,1)|SOX SCRUBBER EXHAUST ACIDITY(15,1)|CAO(13,5)|CARBON DIOXIDE EMISSION REDUCTION(13,1)|SEAWATER SOX SCRUBBER(13,1)|AWL REACTOR PERFORMANCE(12,3)|CONTAINER SHIP(11,3)|CARBON DIOXIDE EMISSION(11,1)|SCRUBBER SORBENT TOWER(11,1)|SEAWATER AEROSOL MIST(11,1)|WATER RESOURCE(11,1)|CARBON DIOXIDE(10,5)|PANAMAX CLASS VESSEL(10,2)|SCRUBBER EFFLUENT WATER(10,2)|AWL REACTOR AWL CHAMBER(10,1)|AWL REACTOR EFFLUENT(10,1)|MULTISTAGE AWL REACTOR(10,1)|SEAWATER SPRAY MIST(10,1)|SOX SCRUBBER EXHAUST GAS(9,2)|SOX SCRUBBER OUTLET(9,1)|AWL EFFLUENT PH(8,1)|MITIGATE ACIDIFICATION(8,1)|SEAWATER ALKALINITY(8,1)|SHIP HEAVY CARGO STABILITY(8,1)|WASTEWATER ACIDIFICATION(8,1)|ADSORBING TOWER(7,1)|SHIP EXHAUST STACK(7,1)|AQUEOUS PHASE(6,5)|EARTH ATMOSPHERE(6,2)|SHIP EXHAUST PORT(6,2)|SOX SCRUBBER WATER DISCHARGE(6,2)|WATER SUPPLY(6,2)|ABUNDANT BICARBONATE(6,1)|AWL REACTOR EQUIPMENT(6,1)|CCS CONTOUR(6,1)|MARINE EXHAUST(6,1)|SOX REACTOR(6,1)|VESSEL CONSTRAINT(6,1)|PCO(5,3)|NONLINEARITY(5,2)|AQUEOUS EFFLUENT OUTLET(5,1)|AWL FLUIDIZED BED REACTOR(5,1)|AWL PH(5,1)|CO2 EMISSION(5,1)|ECONOMIC HEALTH(5,1)|FUEL SULFUR(5,1)|GASEOUS EFFLUENT(5,1)|NONACIDIC SEAWATER SOURCE(5,1)|PACKED BED CHAMBER(5,1)|PACKED BED COLUMN(5,1)|PACKED BED REACTION MEDIA(5,1)|REACTOR PERFORMANCE OPTIMIZATION(5,1)|SCRUBBER PH(5,1)|SULFUR EMISSION(5,1)|BICARBONATE ION(4,4)|AWL PROCESS OPTIMIZATION(4,2)|CACO(4,2)|NONLINEAR RESPONSE(4,2)|SEAWATER FUNCTION(4,2)|ARTIFICIAL CARBON PERMANENT STORAGE(4,1)|AWL REACTION(4,1)|BALLAST PUMP(4,1)|CO2 ISOLATION(4,1)|FUTURE ATMOSPHERIC EMISSION(4,1)|GAS EFFLUENT OUTLET(4,1)|GREENHOUSE GAS POWER(4,1)|SAFE DISCHARGE(4,1)|SHIP VOLUME(4,1)|SOX SCRUBBING TOWER NUMBER(4,1)|SULFATE ION ANDCO(4,1)|BUFFER NATURE(3,1)||(IN202517114935)|CARBON CAPTURE(100,4)|DEACIDIFYING SOX SCRUBBER EFFLUENT(100,1)|SHIP CARBON CAPTURE(100,1)|SOX SCRUBBER(69,32)|MITIGATE ACIDITY(63,5)|AWL REACTOR(61,41)|AWL EFFLUENT OUTLET(61,5)|AQUEOUS EFFLUENT OUTLET(60,9)|SOX EMISSION(60,5)|INTEGRATING AWL(57,3)|SOX EMISSION POLLUTION(53,2)|ABSORBER TOWER(50,10)|GAS EFFLUENT OUTLET(44,6)|LIMESTONE ACCELERATED WEATHERING(43,2)|SOX EFFLUENT(42,1)|SHIP PRODUCING CO2(40,3)|SEAWATER ACIDIFICATION(38,1)|SHIP REACTOR(36,1)|ALLEVIATING CO2(34,2)|FLUID COMMUNICATION(32,10)|SOX SCRUBBING(32,6)|SEQUESTERING CO2(30,5)|MOVING SEAWATER(29,5)|REACTOR(28,17)|REACTION MEDIUM(27,22)|SHIP(27,18)|SEA(24,9)|SHIP EXHAUST(24,4)|SEQUESTERING CARBON DIOXIDE(23,1)|AQUEOUS EFFLUENT(21,9)|SEAWATER FLOW(21,6)|FINE GRAINED SOLID(20,5)|GAS INLET(20,5)|CARBON DIOXIDE SEQUESTRATION(20,3)|INFRASTRUCTURE(20,1)|SEAWATER(19,15)|WATER INLET(17,5)|ARAGONITE(16,5)|SHIP REDUCTION(16,1)|OLIVINE(15,5)|PYROXENE(15,5)|VATERITE(15,5)|POLLUTING EMISSION(15,1)|AWL REACTOR CHAMBER(14,7)|CALCITE(14,5)|DOLOMITE(14,5)|MAFIC ROCK(14,5)|SILICATE(14,5)|CARBON DIOXIDE POLLUTION(13,2)|SOX SCRUBBER EFFLUENT ACIDITY(13,1)|MGSIO(12,5)|NAHCO(12,5)|SOX SCRUBBER AQUEOUS EFFLUENT(12,2)|SHIP SOX SCRUBBER EFFLUENT(12,1)|SAFETY VALVE(11,6)|REAGENT(11,5)|CARGO SHIP(11,2)|SEA LIFE(11,1)|CAO(10,5)|SEAWATER SOX SCRUBBER(10,1)|CARBON DIOXIDE(9,10)|CONTAINER SHIP(8,3)|AWL REACTOR ABILITY(8,2)|SCRUBBER EFFLUENT WATER(8,2)|SHIP EXHAUST STACK(8,2)|ACCOMPANIMENT DATA(8,1)|ACIDIFIED EFFLUENT NEUTRALIZATION(8,1)|AWL REACTOR AWL CHAMBER(8,1)|AWL REACTOR EFFLUENT(8,1)|INCOMING CO2 INCOMPLETE TITRATION(8,1)|SCRUBBER ABSORBER TOWER(8,1)|SHIP EXHAUST CO2 CAPTURE(8,1)|UNDERWAY SEA CHEST(8,1)|AWL REACTOR PERFORMANCE(7,2)|ONBOARD SHIP(7,2)|PANAMAX CO2 EMISSION(7,1)|AWL REACTION MEDIUM(6,4)|AWL EFFLUENT PH(6,1)|AWL OPTIMIZATION(6,1)|CO2 SEQUESTRATION NONLINEARITY(6,1)|PANAMAX SIZED SHIP(6,1)|SEAWATER ALKALINITY(6,1)|SOX ACIDITY(6,1)|SOX SCRUBBER GAS EFFLUENT(6,1)|BULK CARRIER(5,4)|CO2 NONLINEAR RESPONSE(5,2)|LIMESTONE SOLID DISSOLUTION(5,2)|ABUNDANT BICARBONATE(5,1)|ANTHROPOGENIC CO2 GENERATION(5,1)|AWL REACTION PACKED BED(5,1)|AWL REACTOR EQUIPMENT(5,1)|EFFLUENT WATER ACIDITY(5,1)|GENERAL TRADE(5,1)|NONACIDIFIED SEAWATER SOURCE(5,1)|SEAWATER EFFLUENT(5,1)|SHIP CONSTRAINT(5,1)|SHIP EMITTED CO2(5,1)|SHIP WATERLINE(5,1)|SOX REACTOR(5,1)|PCO(4,5)|BALLAST PUMP(4,2)|AMBIENT SEAWATER(4,1)|ANTHROPOGENIC CARBON PERMANENT STORAGE(4,1)|AWL FLUIDIZED BED REACTOR(4,1)|AWL REACTOR REACTION MEDIUM(4,1)|CO2 INTRODUCTION(4,1)|CO2 STREAM(4,1)|EARTH CO2(4,1)|ECONOMIC HEALTH(4,1)|EXTRA SEAWATER(4,1)|FUEL SULFUR(4,1)|GROWING CONCERN(4,1)|ONBOARD AWL PROCESS OPTIMIZATION(4,1)|PACKED BED CHAMBER(4,1)|REACTOR DIMENSION(4,1)|BICARBONATE ION(3,4)|SEAWATER FUNCTION(3,2)|TREND(3,2)|BUFFERING ABILITY(3,1)|CO2 PERMANENT STORAGE(3,1)|EARTH ATMOSPHERE(3,1)|EMISSION STREAM(3,1)|FUTURE RELEASE(3,1)|MULTISTAGE AWL REACTOR DESIGN(3,1)|POTENT GREENHOUSE GAS(3,1)|SCRUBBER AQUEOUS EFFLUENT CAUSE(3,1)|SHIP AMBIENT WATER(3,1)|SOX SCRUBBING TOWER NUMBER(3,1)|SULFURIC ACID ACIDITY(3,1)|SULFURIC ACID PROTON(3,1)|TOTAL SHIP EMISSION(3,1)||(AU2024264529)|SOX EMISSION POLLUTION(100,1)|SOX EMISSION(94,4)|SOX SCRUBBER(93,28)|AWL REACTOR(89,41)|AWL EFFLUENT OUTLET(89,5)|AQUEOUS EFFLUENT OUTLET(88,9)|INTEGRATING AWL(84,3)|MITIGATE ACIDITY(78,4)|ABSORBER TOWER(74,10)|GAS EFFLUENT OUTLET(64,6)|SOX EFFLUENT(62,1)|SHIP PRODUCING CO2(59,3)|SHIP REACTOR(53,1)|ALLEVIATING CO2(50,2)|FLUID COMMUNICATION(47,10)|SOX SCRUBBING(47,6)|SEQUESTERING CO2(44,5)|MOVING SEAWATER(43,5)|SCRUBBER EFFLUENT(41,6)|REACTION MEDIUM(39,22)|SHIP(39,18)|CARBON DIOXIDE SEQUESTRATION(36,1)|SHIP EXHAUST(35,4)|REACTOR(34,15)|AQUEOUS EFFLUENT(30,9)|SEAWATER FLOW(30,6)|INFRASTRUCTURE(30,1)|SEA(29,8)|FINE GRAINED SOLID(29,5)|GAS INLET(29,5)|WATER INLET(26,5)|SEAWATER(23,15)|ARAGONITE(23,5)|OLIVINE(22,5)|PYROXENE(22,5)|VATERITE(22,5)|CALCITE(21,5)|DOLOMITE(21,5)|MAFIC ROCK(21,5)|SILICATE(21,5)|AWL REACTOR CHAMBER(20,7)|CARBON DIOXIDE(20,2)|CARBON DIOXIDE(19,14)|SOX SCRUBBER EFFLUENT ACIDITY(19,1)|MGSIO(18,5)|NA2CO3(18,5)|SOX SCRUBBER AQUEOUS EFFLUENT(18,2)|SHIP SOX SCRUBBER EFFLUENT(18,1)|NAHCO3(17,5)|REAGENT(17,5)|SEA LIFE(17,1)|SAFETY VALVE(16,6)|CAO(15,5)|LIMESTONE ACCELERATED WEATHERING(13,1)|AWL REACTOR ABILITY(12,2)|SCRUBBER EFFLUENT WATER(12,2)|SHIP EXHAUST STACK(12,2)|ACCOMPANIMENT DATA(12,1)|ACIDIFIED EFFLUENT NEUTRALIZATION(12,1)|AWL REACTOR AWL CHAMBER(12,1)|AWL REACTOR EFFLUENT(12,1)|SCRUBBER ABSORBER TOWER(12,1)|SHIP EXHAUST CO2 CAPTURE(12,1)|UNDERWAY SEA CHEST(12,1)|AWL REACTOR PERFORMANCE(11,2)|ONBOARD SHIP(10,2)|PANAMAX CO2 EMISSION(10,1)|AWL REACTION MEDIUM(9,4)|BICARBONATE ION(9,4)|AWL EFFLUENT PH(9,1)|AWL OPTIMIZATION(9,1)|CO2 SEQUESTRATION NONLINEARITY(9,1)|SEAWATER ALKALINITY(9,1)|SOX ACIDITY(9,1)|SOX SCRUBBER GAS EFFLUENT(9,1)|CO2 NONLINEAR RESPONSE(8,2)|ANTHROPOGENIC CO2 GENERATION(8,1)|AWL REACTION PACKED BED(8,1)|EFFLUENT WATER ACIDITY(8,1)|INCOMPLETE TITRATION(8,1)|PANAMAX SHIP(8,1)|SEAWATER EFFLUENT(8,1)|SHIP CONSTRAINT(8,1)|SHIP EMITTED CO2(8,1)|SHIP WATERLINE(8,1)|ABUNDANT BICARBONATE(7,1)|AWL REACTOR EQUIPMENT(7,1)|CACO3 DISSOLUTION(7,1)|EMISSION POLLUTION(7,1)|GENERAL TRADE(7,1)|NONACIDIFIED SEAWATER SOURCE(7,1)|SOX REACTOR(7,1)|SULFUR OXIDE(6,7)|PCO(6,4)|BALLAST PUMP(6,2)|AMBIENT SEAWATER(6,1)|ANTHROPOGENIC CARBON PERMANENT STORAGE(6,1)|AWL FLUIDIZED BED REACTOR(6,1)|AWL REACTOR REACTION MEDIUM(6,1)|CO2 INTRODUCTION(6,1)|CO2 STREAM(6,1)|EARTH CO2(6,1)|ECONOMIC HEALTH(6,1)|EXTRA SEAWATER(6,1)|FUEL SULFUR(6,1)|GROWING CONCERN(6,1)|ONBOARD AWL PROCESS OPTIMIZATION(6,1)|PACKED BED CHAMBER(6,1)|REACTOR DIMENSION(6,1)|LIMESTONE SOLID(5,2)|SEAWATER FUNCTION(5,2)|TREND(5,2)|BUFFERING ABILITY(4,1)|CO2 PERMANENT STORAGE(4,1)|EARTH ATMOSPHERE(4,1)|EMISSION STREAM(4,1)|FUTURE RELEASE(4,1)|MOLL TOTAL CAPTURE(4,1)|MULTISTAGE AWL REACTOR DESIGN(4,1)|NEUTRALIZING(4,1)|POTENT GREENHOUSE GAS(4,1)|SCRUBBER AQUEOUS EFFLUENT CAUSE(4,1)|SHIP AMBIENT WATER(4,1)|SOX SCRUBBING TOWER NUMBER(4,1)|SULFATE ION(4,1)|TOTAL SHIP EMISSION(4,1)|WORLDWIDE CARBON(4,1)|AWL PROCESS REACTOR UPTAKE(3,1)|BUBBLING(3,1)|CAPTURING CARBON DIOXIDE(3,1)| (US20240350972)|1. A reactor for integrating an AWL process with a SOx scrubbing process on a ship producing CO2 and SOx emissions, the reactor comprising:| at least one chamber filled with a reaction medium,| a water inlet in fluid communication with an aqueous effluent outlet of an absorber tower,| a gas inlet in fluid communication with a gas effluent outlet of the absorber tower, an AWL effluent outlet, and| any number of pumps, controls, and safety valves necessary for moving seawater and gas through the reactor at a desired rate.|2. The reactor of claim 1, wherein the absorber tower is a SOx scrubber.|3. The reactor of claim 1, wherein the at least one chamber is filled with the reaction medium in a fashion selected from the group consisting of: fluidized bed, packed bed, and any combination thereof.|4. The reactor of claim 1, wherein the reaction medium comprises a material or reagent selected from the group consisting of: CaO; a carbonate, including its aragonite, calcite and vaterite forms, dolomite, and Na2CO3; NaHCO3; a silicate, including MgSiO3, olivine, pyroxene, mafic rock; another material capable of sequestering CO2, and any combination thereof.|5. The reactor of claim 1, wherein, the reaction medium is CaCO3.|6. The reactor of claim 1, wherein the reaction medium is a fine grained solid.|7. The reactor of claim 1, wherein the reactor comprises a plurality of chambers filled with the reaction medium.|8. The reactor of claim 7, wherein the plurality of chambers is connected in sequence.|9. The reactor of claim 7, wherein the plurality of chambers is connected in parallel.|10. A method for alleviating CO2 and SOx emissions pollution produced by a ship comprising:| installing an AWL reactor aboard the ship, the AWL reactor comprising:| at least one chamber filled with a reaction medium,| a water inlet in fluid communication with an aqueous effluent outlet of a SOx scrubber aboard the ship,| a gas inlet in fluid communication with a gas effluent outlet of the SOx scrubber,| an AWL effluent outlet, and| any number of pumps, controls, and safety valves necessary for moving seawater and gas through the AWL reactor at a desired rate;| flowing seawater from the aqueous effluent outlet and a gas from the gas effluent outlet from the SOx scrubber into the AWL reactor;| to mitigate the acidity of the seawater outflowing from the aqueous effluent outlet, while also safely storing carbon dioxide produced by the ship in the ocean.|11. The method of claim 10, wherein the at least one chamber is filled with the reaction medium in a fashion selected from the group consisting of: fluidized bed, packed bed, and any combination thereof.|12. The method of claim 10, wherein the reaction medium comprises a material or reagent selected from the group consisting of: CaO; a carbonate, including its aragonite, calcite and vaterite forms, dolomite, and Na2CO3; NaHCO3; a silicate, including MgSiO3, olivine, pyroxene, mafic rock; another material capable of sequestering CO2, and any combination thereof.|13. The method of claim 10, wherein the reaction medium is CaCO3.|14. The method of claim 10, wherein the reaction medium is a fine grained solid.|15. The method of claim 10, wherein the AWL reactor comprises a plurality of chambers filled with the reaction medium.|16. The method of claim 15, wherein the plurality of chambers is connected in sequence.|17. The method of claim 15, wherein the plurality of chambers is connected in parallel. (US20240350972)|CROSS-REFERENCE TO RELATED APPLICATIONS|[0001] The present application claims priority under 35 U.S.C. 119 (e) to U.S. Provisional Application No. 63/497,890 filed Apr. 24, 2023, the disclosure of which is incorporated herein by reference in its entirety.|(US20240350972)|FIELD OF THE INVENTION|[0002] The current disclosure is directed to methods of carbon dioxide sequestration, more specifically, to ship-based reactors capable of sequestering carbon dioxide and/or deacidifying SOx scrubber effluent.|BACKGROUND OF THE INVENTION|[0003] Carbon dioxide (CO2) constitutes about 0.04% (400 parts per million) of the atmosphere. Despite its relatively small overall concentration, CO2 is a potent greenhouse gas that plays an important role in regulating the Earth's surface temperature. Presently, anthropogenic CO2 generation is taking place at a rate greater than it is being consumed and/or stored, leading to increasing concentrations of CO2 in the atmosphere. As such, there is a growing concern that rising levels of CO2 in the earth's atmosphere may present a substantial environmental challenge, and an increased interest in developing methods for removing CO2 from emission streams and the atmosphere, as well as storing the removed CO2 in a manner that prevents its future release into the atmosphere. This capture and storage process is collectively known as CO2 sequestration.|[0004] The shipping industry is important for worldwide trade and economic health. Ships, such as container ships and bulk carriers, contribute to worldwide carbon and sulfur output. In response, the International Maritime Organization (IMO) has issued a goal to reduce emissions of sulfur oxides (SOx) by 7-fold. This goal gives ship operators two options: install SOx scrubbers on ships or change to low sulfur fuels. Notably, a typical seawater SOx scrubber functions by intaking the flue gas from a ship's exhaust stack and passing it through a mist of aerosolized seawater pumped from, for example, an underway seachest (as described, for example, in Sasaki et al., Practical Design of Marine SOx Scrubber for Mega-Container Ships, Mitsubishi Heavy Industries Technical Rev. vol. 56, no. 3, (September 2019), the disclosure of which is hereby incorporated by reference in its entirety). As such, SOx from the exhaust gas readily dissolve into the seawater and quickly oxidize to sulfuric acid. In turn, the bicarbonate ions (i.e., the alkalinity) of the seawater are titrated against the protons made from converting SOx into sulfuric acid and, as such, the overall SOx scrubbing process produces sulfate ions and CO2. However, not all of the SOx scrubbing process protons are absorbed by the seawater alkalinity, and the pH of the scrubber effluent may be as low as pH 2-3. Accordingly, while the SOx scrubbers do reduce SOx emissions output, they also acidify their wastewater and also contribute to CO2 emissions. Thus, there exists a great and urgent need for pollution reducing solutions that both reduce the carbon dioxide emissions and alleviate the acidification of water resources.|SUMMARY OF THE INVENTION|[0005] Various embodiments are directed to a reactor for integrating an AWL process with a SOx scrubbing process on a ship producing CO2 and SOx emissions, the reactor including:| - at least one chamber filled with a reaction medium,| - a water inlet in fluid communication with an aqueous effluent outlet of an absorber tower,| - a gas inlet in fluid communication with a gas effluent outlet of the absorber tower, an AWL effluent outlet, and| - any number of pumps, controls, and safety valves necessary for moving seawater and gas through the reactor at a desired rate.|[0010] In various such embodiments, the absorber tower is a SOx scrubber.|[0011] In still various such embodiments, the at least one chamber is filled with the reaction medium in a fashion selected from the group consisting of: fluidized bed, packed bed, and any combination thereof.|[0012] In still yet various embodiments, the reaction medium includes a material or reagent selected from the group consisting of: CaO; a carbonate, including its aragonite, calcite and vaterite forms, dolomite, and Na2CO3; NaHCO3; a silicate, including MgSiO3, olivine, pyroxene, mafic rock; another material capable of sequestering CO2, and any combination thereof.|[0013] In yet still various such embodiments, the reaction medium is CaCO3.|[0014] In yet various such embodiments, the reaction medium is a fine grained solid.|[0015] In various such embodiments, the reactor comprises a plurality of chambers filled with the reaction medium.|[0016] In still various such embodiments, wherein the reactor comprises the plurality of chambers, the plurality of chambers is connected in sequence.|[0017] In yet still various such embodiments, the plurality of chambers is connected in parallel.|[0018] Still various embodiments are directed to a method for alleviating CO2 and SOx emissions pollution produced by a ship including:| - installing an AWL reactor aboard the ship, the AWL reactor including: | - at least one chamber filled with a reaction medium,| - a water inlet in fluid communication with an aqueous effluent outlet of a SOx scrubber aboard the ship,| - a gas inlet in fluid communication with a gas effluent outlet of the SOx scrubber,| - an AWL effluent outlet, and| - any number of pumps, controls, and safety valves necessary for moving seawater and gas through the AWL reactor at a desired rate;|flowing seawater from the aqueous effluent outlet and a gas from the gas effluent outlet from the SOx scrubber into the AWL reactor;|to mitigate the acidity of the seawater outflowing from the aqueous effluent outlet, while also safely storing carbon dioxide produced by the ship in the ocean.|[0025] In various such embodiments, the at least one chamber is filled with the reaction medium in a fashion selected from the group consisting of: fluidized bed, packed bed, and any combination thereof.|[0026] In still various such embodiments, the reaction medium includes a material or reagent selected from the group consisting of: CaO; a carbonate, including its aragonite, calcite and vaterite forms, dolomite, and Na2CO3; NaHCO3; a silicate, including MgSiO3, olivine, pyroxene, mafic rock; another material capable of sequestering CO2, and any combination thereof.|[0027] In still yet various embodiments, the reaction medium is CaCO3.|[0028] In yet still various such embodiments, the reaction medium is a fine grained solid.|[0029] In yet still various such embodiments, the AWL reactor comprises a plurality of chambers filled with the reaction medium.|[0030] In various such embodiments, the plurality of chambers is connected in sequence.|[0031] In still various such embodiments, the plurality of chambers is connected in parallel.|[0032] Additional embodiments and features are set forth in part in the description that follows, and in part will become apparent to those skilled in the art upon examination of the specification or may be learned by the practice of the disclosed subject matter. A further understanding of the nature and advantages of the present disclosure may be realized by reference to the remaining portions of the specification and the drawings, which forms a part of this disclosure.|(US20240350972)|BRIEF DESCRIPTION OF THE DRAWINGS|[0033] These and other features and advantages of the present invention will be better understood by reference to the following detailed description when considered in conjunction with the accompanying data and figures, wherein:|[0034] FIGS. 1A and 1B schematically illustrate examples of basic AWL reactor designs, in accordance with embodiments of the application.|[0035] FIGS. 2A and 2B schematically illustrate multi-stage AWL reactor designs, in accordance with embodiments of the application.|[0036] FIG. 3 provides illustrative model data plots showing the pH values of the effluent exiting the first and second chambers of the AWL reactor as a function of the seawater and flue gas flow rates, in accordance with embodiments of the application.|[0037] FIG. 4 provides illustrative model data showing an advantage of splitting water flow into two streams, in accordance with embodiments of the application.|[0038] FIG. 5 provides illustrative model data for the overall performance of the AWL reactors when plumbed to the effluent of SOx scrubbers, in accordance with embodiments of the application.|[0039] FIG. 6A provides data showing the amount of CO2 stored as a function of the volume needed onboard ship for various seawater flows that do not pass through a SOx scrubber; while FIG. 6B shows the same range of seawater flows, but taking advantage of the non-linear response of CO2 sequestered to seawater flow rate, in accordance with embodiments of the application.|(US20240350972)|DETAILED DISCLOSURE|[0040] The embodiments of the invention described herein are not intended to be exhaustive or to limit the invention to precise forms disclosed. Rather, the embodiments selected for description have been chosen to enable one skilled in the art to practice the invention.|[0041] Turning to the drawings, schemes, and data, embodiments of reactor systems and methods for capturing carbon dioxide emitted by ships and permanently storing it in the ocean are provided. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) in order to sequester carbon. Certain embodiments may also be used to mitigate the acidity of the effluent of a ship's SOx scrubbers, while some embodiments solve both issues (i.e., water acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely disposed of into the ambient water.|[0042] A conventional AWL process/reactor uptakes CO2 gas and reacts it with CaCO3 (commonly known as limestone) in water (often seawater) according to, most generally, the reaction equation:|which results in safe and permanent storage of anthropogenic carbon in the ocean as bicarbonate ions. This is the natural buffering process, sometimes called ‘carbonate compensation’ that regulates earth's CO2 concentration in the atmosphere. However, this process is constrained by 2 rate limiting steps-CO2 gas adsorption and limestone solids dissolution. More specifically, since AWL processes typically rely on an oversupply of CO2 as compared to ambient air (i.e., a partial pressure of CO2 gas (pCO2) higher than the ambient levels of CO2), CO2 gas adsorption by an AWL reactor's reaction medium (e.g., limestone) is often faster than the dissolution of that reactor's reaction medium's solids, resulting in an incomplete titration of the incoming CO2.|[0043] This application is directed to embodiments of a reactor and a method for integrating an AWL process with a SOx scrubbing process on a ship producing CO2 and SOx emissions, such as to mitigate the acidity of the aqueous effluent of the SOx scrubbing process, while also safely storing carbon dioxide from the ship's exhaust in the ocean. More specifically, in many embodiments, the aqueous (e.g., seawater-based) effluent of a ship's SOx scrubber is fed into an AWL reactor, along with, optionally, the gas effluent of the same SOx scrubber (potentially still containing a portion of the ship's exhaust CO2 that escaped being dissolved in the aqueous effluent), wherein the SOx scrubber's aqueous and gas effluents are contacted with an AWL reaction medium, such as, for example, limestone, disposed within a chamber of the AWL reactor. As such, in many embodiments, upon contact with the AWL reaction medium, both the sulfuric acid protons from the SOx scrubber's aqueous effluent and CO2 from the ship's flue gas react with the reaction medium to produce bicarbonate ions (HCO3−) in solution to be released into the ship's surrounding water for safe and permanent storage of CO2 in the ocean. In some embodiments, the SOx scrubber is any absorber tower functioning similarly to a SOx scrubber—i.e., intaking exhaust gas from a ship's exhaust and passing it through a mist of aerosolized seawater to absorb the exhaust gases, including CO2, into the seawater to be fed into the AWL reactor of embodiments.|[0044] FIGS. 1A and 1B provide examples of the most basic AWL reactors of many embodiments. To this end, in many embodiments, the AWL reactor at least comprises: at least one chamber filled with the AWL reaction medium (e.g., limestone), a water inlet in fluid communication with an aqueous effluent outlet of the SOx scrubber (FIG. 1A) or another absorber tower (FIG. 1B), a gas inlet in fluid communication with a gas effluent of the SOx scrubber (FIG. 1A), an AWL effluent outlet, and any number of pumps, controls, and safety valves necessary for moving seawater and gas through the reactor at a desired rate. In many embodiments, the at least one chamber is filled with the reaction medium in a fashion selected from the group consisting of: fluidized bed (FIG. 1A), packed bed (FIG. 1B), and any combination thereof. In some embodiments the packed bed chamber is as long as 20 meters or longer, and as thick as 0.15 m or thicker. In many embodiments, the AWL reaction medium comprises a material or reagent selected from the group consisting of: CaO; a carbonate, including its aragonite, calcite and vaterite forms, dolomite, and Na2CO3; NaHCO3; a silicate, including MgSiO3, olivine, pyroxene, mafic rock; another material capable of sequestering CO2, and any combination thereof. In many embodiments, the reaction medium is CaCO3 (limestone). In many embodiments, the reaction medium is a fine grained solid. Accordingly, in many embodiments, the aqueous/seawater effluent of a ship's SOx scrubber or another gas absorbing implement is flown into the AWL reactor, along with some optional amount of the same SOx scrubber's gas effluent, wherein the seawater effluent and gas are mixed and contacted with the reaction medium disposed within the at least one of the AWL reactor's chambers, before being released into the ocean as an AWL effluent rich in bicarbonate ions, thus reducing the acidity of the SOx scrubber's effluent and safely and permanently storing the ship's emitted CO2 in the ocean.|[0045] In many embodiments, the SOx scrubber's aqueous effluent is the only source of the seawater feed into the AWL reactor and, thus, defines the flow rate of water through the AWL reactor according to the pre-existing flow rate of the SOx scrubber. In some such embodiments, the SOx scrubber′ gas effluent is then used to adjust the flow rate of gas through the AWL reactor as needed to optimize the conditions of the AWL process and the performance of the AWL reactor to capture the most CO2 at the lowest cost. However, in some embodiments, any additional amount of seawater is pumped into the AWL reactor directly from the ship's ambient water as needed to optimize the AWL process and reactor performance.|[0046] In many embodiments, the AWL process and reactor are multi-stage, incorporating any number of SOx scrubbing towers and AWL chambers to achieve the most efficient and effective capture of the ship's exhaust CO2 within constraints of a ship. For example, FIGS. 2A and 2B show examples of such multi-stage AWL reactors of many embodiments. More specifically, FIG. 2A illustrates the AWL reactor of many embodiments comprising two consecutively connected AWL reactor chambers, wherein the aqueous effluent from the SOx scrubber first enters a first AWL chamber, where most of the aqueous effluent's acidity and some CO2 are removed from the effluent, and is then flown into a second AWL chamber to remove additional carbon dioxide from the effluent. Furthermore, in this particular example, the gas effluent coming off the SOx scrubber is split into two parallel streams, where a first portion of the gas effluent is pumped into the first AWL chamber and a second portion of the gas effluent is pumped into the second AWL chamber, in order to facilitate the control over the gas flow rate through the AWL chambers and enable the optimization of the AWL process of many embodiments.|[0047] On the other hand, FIG. 2B illustrates an alternative set-up of the AWL reactor of many embodiments, wherein the AWL reactor comprises a plurality of AWL chambers (here, packed beds of the AWL reaction medium) connected in parallel. In some embodiments, the AWL reactor is a stack of at least five such packed bed columns comprising the reaction medium, each 20 meters long and 0.15 meters thick, to the overall reactor dimensions of 20 x 0.75 x 0.15 meters. In this particular example, the aqueous effluent from the SOx scrubber (here, absorber tower) is split into multiple streams flown through the plurality of AWL chambers. In many embodiments, the set-up illustrated in FIG. 2B allows to compensate for the mismatch between the rates of the CO2 gas adsorption into the aqueous effluent and limestone solids dissolution, thus, greatly improving the overall efficiency of the AWL process of many embodiments.|[0048] In general, in many embodiments, any number of AWL chambers are interconnected in any way (including in sequence or in parallel) with any number of SOx scrubbers, SOx scrubber-type absorber towers, and ship's exhaust as needed to optimize the water and gas flow rates, such as to achieve the most efficient AWL process and capture most carbon dioxide at the lowest cost. However, it should be noted here, that reversing the flow of the aqueous effluent from the AWL reactor/chambers to the SOx scrubber in particular is not advisable, as the SOx scrubbing process may acidify the aqueous effluent, thus eliminating any benefit to the buffering ability of the AWL reaction medium (e.g., limestone). In addition, in many embodiments, a variety of pumps, monitors, and safety valves are added for the same purpose. In many embodiments, the AWL reactor is positioned within the ship below the ship's waterline. In many such embodiments, any additional seawater that may be needed for optimization of the onboard AWL processes may be delivered to the AWL reactor by virtue of the ship's movement across water, without any need for additional pumps.|EXEMPLARY EMBODIMENTS|[0049] Although the following embodiments provide details on certain embodiments of the inventions, it should be understood that these are only exemplary in nature, and are not intended to limit the scope of the invention. (US20240350972)|CROSS-REFERENCE TO RELATED APPLICATIONS|[0001] The present application claims priority under 35 U.S.C. 119 (e) to U.S. Provisional Application No. 63/497,890 filed Apr. 24, 2023, the disclosure of which is incorporated herein by reference in its entirety.|(US20240350972)|FIELD OF THE INVENTION|[0002] The current disclosure is directed to methods of carbon dioxide sequestration, more specifically, to ship-based reactors capable of sequestering carbon dioxide and/or deacidifying SOx scrubber effluent.|BACKGROUND OF THE INVENTION|[0003] Carbon dioxide (CO2) constitutes about 0.04% (400 parts per million) of the atmosphere. Despite its relatively small overall concentration, CO2 is a potent greenhouse gas that plays an important role in regulating the Earth's surface temperature. Presently, anthropogenic CO2 generation is taking place at a rate greater than it is being consumed and/or stored, leading to increasing concentrations of CO2 in the atmosphere. As such, there is a growing concern that rising levels of CO2 in the earth's atmosphere may present a substantial environmental challenge, and an increased interest in developing methods for removing CO2 from emission streams and the atmosphere, as well as storing the removed CO2 in a manner that prevents its future release into the atmosphere. This capture and storage process is collectively known as CO2 sequestration.|[0004] The shipping industry is important for worldwide trade and economic health. Ships, such as container ships and bulk carriers, contribute to worldwide carbon and sulfur output. In response, the International Maritime Organization (IMO) has issued a goal to reduce emissions of sulfur oxides (SOx) by 7-fold. This goal gives ship operators two options: install SOx scrubbers on ships or change to low sulfur fuels. Notably, a typical seawater SOx scrubber functions by intaking the flue gas from a ship's exhaust stack and passing it through a mist of aerosolized seawater pumped from, for example, an underway seachest (as described, for example, in Sasaki et al., Practical Design of Marine SOx Scrubber for Mega-Container Ships, Mitsubishi Heavy Industries Technical Rev. vol. 56, no. 3, (September 2019), the disclosure of which is hereby incorporated by reference in its entirety). As such, SOx from the exhaust gas readily dissolve into the seawater and quickly oxidize to sulfuric acid. In turn, the bicarbonate ions (i.e., the alkalinity) of the seawater are titrated against the protons made from converting SOx into sulfuric acid and, as such, the overall SOx scrubbing process produces sulfate ions and CO2. However, not all of the SOx scrubbing process protons are absorbed by the seawater alkalinity, and the pH of the scrubber effluent may be as low as pH 2-3. Accordingly, while the SOx scrubbers do reduce SOx emissions output, they also acidify their wastewater and also contribute to CO2 emissions. Thus, there exists a great and urgent need for pollution reducing solutions that both reduce the carbon dioxide emissions and alleviate the acidification of water resources.|SUMMARY OF THE INVENTION|[0005] Various embodiments are directed to a reactor for integrating an AWL process with a SOx scrubbing process on a ship producing CO2 and SOx emissions, the reactor including:| - at least one chamber filled with a reaction medium,| - a water inlet in fluid communication with an aqueous effluent outlet of an absorber tower,| - a gas inlet in fluid communication with a gas effluent outlet of the absorber tower, an AWL effluent outlet, and| - any number of pumps, controls, and safety valves necessary for moving seawater and gas through the reactor at a desired rate.|[0010] In various such embodiments, the absorber tower is a SOx scrubber.|[0011] In still various such embodiments, the at least one chamber is filled with the reaction medium in a fashion selected from the group consisting of: fluidized bed, packed bed, and any combination thereof.|[0012] In still yet various embodiments, the reaction medium includes a material or reagent selected from the group consisting of: CaO; a carbonate, including its aragonite, calcite and vaterite forms, dolomite, and Na2CO3; NaHCO3; a silicate, including MgSiO3, olivine, pyroxene, mafic rock; another material capable of sequestering CO2, and any combination thereof.|[0013] In yet still various such embodiments, the reaction medium is CaCO3.|[0014] In yet various such embodiments, the reaction medium is a fine grained solid.|[0015] In various such embodiments, the reactor comprises a plurality of chambers filled with the reaction medium.|[0016] In still various such embodiments, wherein the reactor comprises the plurality of chambers, the plurality of chambers is connected in sequence.|[0017] In yet still various such embodiments, the plurality of chambers is connected in parallel.|[0018] Still various embodiments are directed to a method for alleviating CO2 and SOx emissions pollution produced by a ship including:| - installing an AWL reactor aboard the ship, the AWL reactor including: | - at least one chamber filled with a reaction medium,| - a water inlet in fluid communication with an aqueous effluent outlet of a SOx scrubber aboard the ship,| - a gas inlet in fluid communication with a gas effluent outlet of the SOx scrubber,| - an AWL effluent outlet, and| - any number of pumps, controls, and safety valves necessary for moving seawater and gas through the AWL reactor at a desired rate;|flowing seawater from the aqueous effluent outlet and a gas from the gas effluent outlet from the SOx scrubber into the AWL reactor;|to mitigate the acidity of the seawater outflowing from the aqueous effluent outlet, while also safely storing carbon dioxide produced by the ship in the ocean.|[0025] In various such embodiments, the at least one chamber is filled with the reaction medium in a fashion selected from the group consisting of: fluidized bed, packed bed, and any combination thereof.|[0026] In still various such embodiments, the reaction medium includes a material or reagent selected from the group consisting of: CaO; a carbonate, including its aragonite, calcite and vaterite forms, dolomite, and Na2CO3; NaHCO3; a silicate, including MgSiO3, olivine, pyroxene, mafic rock; another material capable of sequestering CO2, and any combination thereof.|[0027] In still yet various embodiments, the reaction medium is CaCO3.|[0028] In yet still various such embodiments, the reaction medium is a fine grained solid.|[0029] In yet still various such embodiments, the AWL reactor comprises a plurality of chambers filled with the reaction medium.|[0030] In various such embodiments, the plurality of chambers is connected in sequence.|[0031] In still various such embodiments, the plurality of chambers is connected in parallel.|[0032] Additional embodiments and features are set forth in part in the description that follows, and in part will become apparent to those skilled in the art upon examination of the specification or may be learned by the practice of the disclosed subject matter. A further understanding of the nature and advantages of the present disclosure may be realized by reference to the remaining portions of the specification and the drawings, which forms a part of this disclosure.|(US20240350972)|BRIEF DESCRIPTION OF THE DRAWINGS|[0033] These and other features and advantages of the present invention will be better understood by reference to the following detailed description when considered in conjunction with the accompanying data and figures, wherein:|[0034] FIGS. 1A and 1B schematically illustrate examples of basic AWL reactor designs, in accordance with embodiments of the application.|[0035] FIGS. 2A and 2B schematically illustrate multi-stage AWL reactor designs, in accordance with embodiments of the application.|[0036] FIG. 3 provides illustrative model data plots showing the pH values of the effluent exiting the first and second chambers of the AWL reactor as a function of the seawater and flue gas flow rates, in accordance with embodiments of the application.|[0037] FIG. 4 provides illustrative model data showing an advantage of splitting water flow into two streams, in accordance with embodiments of the application.|[0038] FIG. 5 provides illustrative model data for the overall performance of the AWL reactors when plumbed to the effluent of SOx scrubbers, in accordance with embodiments of the application.|[0039] FIG. 6A provides data showing the amount of CO2 stored as a function of the volume needed onboard ship for various seawater flows that do not pass through a SOx scrubber; while FIG. 6B shows the same range of seawater flows, but taking advantage of the non-linear response of CO2 sequestered to seawater flow rate, in accordance with embodiments of the application.|(US20240350972)|DETAILED DISCLOSURE|[0040] The embodiments of the invention described herein are not intended to be exhaustive or to limit the invention to precise forms disclosed. Rather, the embodiments selected for description have been chosen to enable one skilled in the art to practice the invention.|[0041] Turning to the drawings, schemes, and data, embodiments of reactor systems and methods for capturing carbon dioxide emitted by ships and permanently storing it in the ocean are provided. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) in order to sequester carbon. Certain embodiments may also be used to mitigate the acidity of the effluent of a ship's SOx scrubbers, while some embodiments solve both issues (i.e., water acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely disposed of into the ambient water.|[0042] A conventional AWL process/reactor uptakes CO2 gas and reacts it with CaCO3 (commonly known as limestone) in water (often seawater) according to, most generally, the reaction equation:|which results in safe and permanent storage of anthropogenic carbon in the ocean as bicarbonate ions. This is the natural buffering process, sometimes called ‘carbonate compensation’ that regulates earth's CO2 concentration in the atmosphere. However, this process is constrained by 2 rate limiting steps-CO2 gas adsorption and limestone solids dissolution. More specifically, since AWL processes typically rely on an oversupply of CO2 as compared to ambient air (i.e., a partial pressure of CO2 gas (pCO2) higher than the ambient levels of CO2), CO2 gas adsorption by an AWL reactor's reaction medium (e.g., limestone) is often faster than the dissolution of that reactor's reaction medium's solids, resulting in an incomplete titration of the incoming CO2.|[0043] This application is directed to embodiments of a reactor and a method for integrating an AWL process with a SOx scrubbing process on a ship producing CO2 and SOx emissions, such as to mitigate the acidity of the aqueous effluent of the SOx scrubbing process, while also safely storing carbon dioxide from the ship's exhaust in the ocean. More specifically, in many embodiments, the aqueous (e.g., seawater-based) effluent of a ship's SOx scrubber is fed into an AWL reactor, along with, optionally, the gas effluent of the same SOx scrubber (potentially still containing a portion of the ship's exhaust CO2 that escaped being dissolved in the aqueous effluent), wherein the SOx scrubber's aqueous and gas effluents are contacted with an AWL reaction medium, such as, for example, limestone, disposed within a chamber of the AWL reactor. As such, in many embodiments, upon contact with the AWL reaction medium, both the sulfuric acid protons from the SOx scrubber's aqueous effluent and CO2 from the ship's flue gas react with the reaction medium to produce bicarbonate ions (HCO3−) in solution to be released into the ship's surrounding water for safe and permanent storage of CO2 in the ocean. In some embodiments, the SOx scrubber is any absorber tower functioning similarly to a SOx scrubber—i.e., intaking exhaust gas from a ship's exhaust and passing it through a mist of aerosolized seawater to absorb the exhaust gases, including CO2, into the seawater to be fed into the AWL reactor of embodiments.|[0044] FIGS. 1A and 1B provide examples of the most basic AWL reactors of many embodiments. To this end, in many embodiments, the AWL reactor at least comprises: at least one chamber filled with the AWL reaction medium (e.g., limestone), a water inlet in fluid communication with an aqueous effluent outlet of the SOx scrubber (FIG. 1A) or another absorber tower (FIG. 1B), a gas inlet in fluid communication with a gas effluent of the SOx scrubber (FIG. 1A), an AWL effluent outlet, and any number of pumps, controls, and safety valves necessary for moving seawater and gas through the reactor at a desired rate. In many embodiments, the at least one chamber is filled with the reaction medium in a fashion selected from the group consisting of: fluidized bed (FIG. 1A), packed bed (FIG. 1B), and any combination thereof. In some embodiments the packed bed chamber is as long as 20 meters or longer, and as thick as 0.15 m or thicker. In many embodiments, the AWL reaction medium comprises a material or reagent selected from the group consisting of: CaO; a carbonate, including its aragonite, calcite and vaterite forms, dolomite, and Na2CO3; NaHCO3; a silicate, including MgSiO3, olivine, pyroxene, mafic rock; another material capable of sequestering CO2, and any combination thereof. In many embodiments, the reaction medium is CaCO3 (limestone). In many embodiments, the reaction medium is a fine grained solid. Accordingly, in many embodiments, the aqueous/seawater effluent of a ship's SOx scrubber or another gas absorbing implement is flown into the AWL reactor, along with some optional amount of the same SOx scrubber's gas effluent, wherein the seawater effluent and gas are mixed and contacted with the reaction medium disposed within the at least one of the AWL reactor's chambers, before being released into the ocean as an AWL effluent rich in bicarbonate ions, thus reducing the acidity of the SOx scrubber's effluent and safely and permanently storing the ship's emitted CO2 in the ocean.|[0045] In many embodiments, the SOx scrubber's aqueous effluent is the only source of the seawater feed into the AWL reactor and, thus, defines the flow rate of water through the AWL reactor according to the pre-existing flow rate of the SOx scrubber. In some such embodiments, the SOx scrubber′ gas effluent is then used to adjust the flow rate of gas through the AWL reactor as needed to optimize the conditions of the AWL process and the performance of the AWL reactor to capture the most CO2 at the lowest cost. However, in some embodiments, any additional amount of seawater is pumped into the AWL reactor directly from the ship's ambient water as needed to optimize the AWL process and reactor performance.|[0046] In many embodiments, the AWL process and reactor are multi-stage, incorporating any number of SOx scrubbing towers and AWL chambers to achieve the most efficient and effective capture of the ship's exhaust CO2 within constraints of a ship. For example, FIGS. 2A and 2B show examples of such multi-stage AWL reactors of many embodiments. More specifically, FIG. 2A illustrates the AWL reactor of many embodiments comprising two consecutively connected AWL reactor chambers, wherein the aqueous effluent from the SOx scrubber first enters a first AWL chamber, where most of the aqueous effluent's acidity and some CO2 are removed from the effluent, and is then flown into a second AWL chamber to remove additional carbon dioxide from the effluent. Furthermore, in this particular example, the gas effluent coming off the SOx scrubber is split into two parallel streams, where a first portion of the gas effluent is pumped into the first AWL chamber and a second portion of the gas effluent is pumped into the second AWL chamber, in order to facilitate the control over the gas flow rate through the AWL chambers and enable the optimization of the AWL process of many embodiments.|[0047] On the other hand, FIG. 2B illustrates an alternative set-up of the AWL reactor of many embodiments, wherein the AWL reactor comprises a plurality of AWL chambers (here, packed beds of the AWL reaction medium) connected in parallel. In some embodiments, the AWL reactor is a stack of at least five such packed bed columns comprising the reaction medium, each 20 meters long and 0.15 meters thick, to the overall reactor dimensions of 20 x 0.75 x 0.15 meters. In this particular example, the aqueous effluent from the SOx scrubber (here, absorber tower) is split into multiple streams flown through the plurality of AWL chambers. In many embodiments, the set-up illustrated in FIG. 2B allows to compensate for the mismatch between the rates of the CO2 gas adsorption into the aqueous effluent and limestone solids dissolution, thus, greatly improving the overall efficiency of the AWL process of many embodiments.|[0048] In general, in many embodiments, any number of AWL chambers are interconnected in any way (including in sequence or in parallel) with any number of SOx scrubbers, SOx scrubber-type absorber towers, and ship's exhaust as needed to optimize the water and gas flow rates, such as to achieve the most efficient AWL process and capture most carbon dioxide at the lowest cost. However, it should be noted here, that reversing the flow of the aqueous effluent from the AWL reactor/chambers to the SOx scrubber in particular is not advisable, as the SOx scrubbing process may acidify the aqueous effluent, thus eliminating any benefit to the buffering ability of the AWL reaction medium (e.g., limestone). In addition, in many embodiments, a variety of pumps, monitors, and safety valves are added for the same purpose. In many embodiments, the AWL reactor is positioned within the ship below the ship's waterline. In many such embodiments, any additional seawater that may be needed for optimization of the onboard AWL processes may be delivered to the AWL reactor by virtue of the ship's movement across water, without any need for additional pumps.|EXEMPLARY EMBODIMENTS|[0049] Although the following embodiments provide details on certain embodiments of the inventions, it should be understood that these are only exemplary in nature, and are not intended to limit the scope of the invention.|(US20240350972)|Example 1: Acid Neutralization|[0050] Background: Ambient seawater that moves into the SOx scrubber is at a pH of 7.8-8.1 in the open ocean. The pH of the aqueous effluent coming out of the SOx scrubber, without any dilution by extra seawater, is pH is 2-3. Thus, neutralizing the SOx effluent is important to avoid damage to sea life and/or infrastructure.|[0051] Methods: To explore the scope of acid neutralization and carbon sequestration by the AWL reactor of many embodiments a series of calculations were performed. In particular, first, the chemistry, especially the pH of the water, before and after the addition of the AWL fluidized bed reactor shown in FIG. 2A to a Panamax sized ship producing 64,000 kg/hr of exhaust with a CO2 concentration of 5% was documented. Here, the reference SOx scrubber had a seawater flow of 700 m3/hr or ˜200 L/sec.|[0052] Results: FIG. 3 provides plots showing the pH of the AWL effluent coming out of the first and second AWL chambers of the AWL reactor, respectively, as a function of the aqueous effluent and gas effluent flow rates. Here, the AWL effluent from the first chamber has a pH between 6.56 and 6.74, representing substantial neutralization of the sulfuric acid acidity generated by the SOx scrubber. Furthermore, the AWL effluent from the second AWL chamber shows the same pH range with slightly lower values at the same seawater and gas flux rates due to the introduction of fresh CO2 from the ship's exhaust stack.|[0053] Conclusions: This example illustrates the ability of the AWL reactor to neutralize acidified effluent exiting a SOx scrubber.|Example 2: Carbon Capture|[0054] Background: The acidity of the SOx scrubber's aqueous effluent causes abundant bicarbonate (HCO3−) and carbonate (CO32−) ions to be converted to carbonic acid (H2CO3) and, correspondingly, CO2, which, in turn, affords high partial pressure of CO2 (pCO2) in the SOx scrubber's effluent, as compared to the flue gas. As such, the first chamber of the AWL reactor as depicted in FIG. 2A does not receive all the CO2 leaving the ship's exhaust, as it bubbles out from the SOx effluent due to high pCO2.|[0055] Methods: It is possible to calculate the total amount of carbon dioxide captured and stored in the AWL reactor's effluent as a function of the gas and water flow rates.|[0056] Results: Once the reactor gets to steady-state there has been enough CaCO3 dissolution to increase the alkalinity and drop the pCO2 below the flue gas value, but the total carbon stored is less than would be predicted from the alkalinity increase alone. By bubbling in another stream of CO2-containing flue gas to the aqueous effluent of the first chamber of the AWL reactor water more carbon dioxide is stored in the second chamber, but the amount drops off because now the pCO2 is large without the water being low in pH. Overall, the calculated rate of carbon capture and sequestration is 0.54 mol/s, which is 2.71% of the 20 mol/s coming through the flue gas. Accordingly, in many embodiments, it is advantageous to split the 200 L/s of water flow into two 100 L/s streams because the lines of constant CCS are closer together at small water flows than they are at larger flow, as illustrated in FIG. 4. This slight non-linearity means 2x 100 L/s streams into two separate pairs of reactors would yield 0.64 mol/s total capture and storage rate, or 3.22% of the total ship's emissions.|[0057] The overall performance of the AWL reactor of many embodiments when plumbed to the effluent of SOx scrubbers can be summarized as a function of gas flow and the volume occupied by AWL reactors and the necessary limestone, as illustrated in FIG. 5. The three different shades in this figure represent: Std case with 45 m3 volume reactor and Kla (the gas transfer coefficient)=0.2/sec (blue), 7.5 m3 reactor with Kla=0.2/see (orange), and 7.5 m3 reactor with Kla=0.6/sec (gray). The two sets of trends are for 2 x 100 L/s (higher CO2 storage rates but larger volumes) and 1 x 200 L/s through a single reactor. These different sensitivities arise from the non-linearity of CO2 sequestration with seawater flow rate. Points along each trend are from varying the gas flow rate from 500-4,000 L/s.|[0058] Conclusions: This example illustrates the ability of the AWL reactor to capture carbon dioxide from the SOx scrubber's effluent.|Example 3: Carbon Capture Without Using A SOx Scrubber|[0059] Background: Certain ships may need carbon sequestration without using SOx scrubber's effluent, such as when using low-sulfur fuels and/or if there is no practical means to connect a SOx reactor to an AWL reactor. For instance, bulk carriers have 2 x 1,000 m3/hr pumps on board for use at port during loading and unloading. These pumps move ballast seawater to ensure the ship is stable as heavy loads are added to, or removed from, the ship while at the dock.|[0060] Methods: By using these pumps while the ship is underway, it is possible to calculate the amount of carbon stored as a function of seawater and gas flow rates. For 400, 600, and 800 L/s of seawater flows and 4000 L/s of exhaust gas flow the amount of CO2 stored as a function of the volume needed onboard ship is shown in FIG. 6.|[0061] Results: Each set of three seawater flows form a set of dots along a line where the size of a reactor and the gas exchange coefficient (Kla) are changed in the model. These embodiments can sequester 7% of a Panamax's CO2 emissions using the 2 x 1,000 m3/hr ballast pumps and taking ˜140 m3 of space on the ship. As these ships have ˜50,000 m3 of cargo space the AWL reactor equipment could be thought of as non-invasive. In addition, FIG. 7 shows modeling results for the same range of seawater flows as FIG. 6, but now taking advantage of the non-linear response of CO2 sequestered to seawater flow rate. As such, the AWL reactor of many embodiments can sequester ˜11% of the CO2 using 350 m3 of space on the vessel.|[0062] Conclusions: This example illustrates the ability of the AWL reactor of many embodiments to capture carbon dioxide by using ballast pumps or another source of non-acidified seawater.|DOCTRINE OF EQUIVALENTS|[0063] This description of the invention has been presented for the purposes of illustration and description. It is not intended to be exhaustive or to limit the invention to the precise form described, and many modifications and variations are possible in light of the teaching above. The embodiments were chosen and described in order to best explain the principles of the invention and its practical applications. This description will enable others skilled in the art to best utilize and practice the invention in various embodiments and with various modifications as are suited to a particular use. The scope of the invention is defined by the following claims. Family Number|(115038942)|115038942|Abstract|(US20240350972 A1)|Many embodiments are directed to reactors and methods for reducing ship exhaust polluting emissions. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) for carbon dioxide sequestration. Certain embodiments may also be used to mitigate high acidity of SOx scrubber effluents, while some embodiments solve both issues (i.e., seawater acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely and permanently stored in the ocean.|(WO2024226673 A3)|De nombreux modes de réalisation concernent des réacteurs et des procédés pour réduire les émissions polluantes de gaz d'échappement de navires. Un grand nombre de ces modes de réalisation concernent des réacteurs mettant en œuvre une altération accélérée de calcaire (AWL) pour la séquestration de dioxyde de carbone. Certains modes de réalisation peuvent également être utilisés pour atténuer l'acidité élevée d'effluents d'absorbeurs-neutraliseurs de SOx, tandis que certains modes de réalisation résolvent les deux problèmes (c'est-à-dire, l'acidification de l'eau de mer et la pollution au dioxyde de carbone). De nombreux modes de réalisation sont mis en œuvre sur des navires cargo (par exemple, des navires porte-conteneurs et/ou des vraquiers) et font appel à de l'eau de mer. Certains modes de réalisation peuvent utiliser un effluent d'un ou de plusieurs absorbeurs-neutraliseurs de SOx en tant que source d'eau de mer pour décarboner et/ou neutraliser l'eau avant qu'elle soit stockée en toute sécurité et en permanence dans l'océan.|Many embodiments are directed to reactors and methods for reducing ship exhaust polluting emissions. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) for carbon dioxide sequestration. Certain embodiments may also be used to mitigate high acidity of SOx scrubber effluents, while some embodiments solve both issues (i.e., seawater acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely and permanently stored in the ocean.|(AU2024264529 A1)|Many embodiments are directed to reactors and methods for reducing ship exhaust polluting emissions. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) for carbon dioxide sequestration. Certain embodiments may also be used to mitigate high acidity of SOx scrubber effluents, while some embodiments solve both issues (i.e., seawater acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely and permanently stored in the ocean.|(IN202517114935 A)|Many embodiments are directed to reactors and methods for reducing ship exhaust polluting emissions. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) for carbon dioxide sequestration. Certain embodiments may also be used to mitigate high acidity of SOx scrubber effluents, while some embodiments solve both issues (i.e., seawater acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely and permanently stored in the ocean.|(CN121605002 A)|Many embodiments relate to reactors and methods for reducing ship exhaust gas pollution emissions . Many such embodiments relate to reactors that implement limestone Accelerated Weathering ( AWL ) to achieve carbon dioxide sequestration . Some embodiments may also be used to mitigate the high acidity of the SO x scrubber effluent , while some embodiments address two issues ( i . e . , sea water acidification and carbon dioxide pollution ) . Many embodiments are implemented on cargo ships ( e . g . , container ships and / or bulk carriers ) and use seawater . Some embodiments may utilize the effluent from one or more SO x scrubbers as a seawater source to decarbonize and / or neutralize the water , which is then safely and permanently stored in the ocean . |(KR20260027884 A)|A number of embodiments are directed to a reactor and method for reducing contaminated emissions of vessel exhaust. Many of these embodiments relate to reactors that implement limestone accelerated weathering (AWL) for carbon dioxide sequestration. Some embodiments may also be used to mitigate the high acidity of SOx scrubber effluent, and some embodiments address both problems (i.e., the acidification of seawater and carbon dioxide contamination). A number of embodiments are implemented in a cargo ship (e.g., a container ship and/or a bulk ship) and use seawater. In certain embodiments, discharge water from one or more SOx scrubbers may be utilized as a source of seawater to decarbonize and/or neutralize the seawater prior to safe and permanent storage in the ocean.|(EP4705006 A2)|Many embodiments are directed to reactors and methods for reducing ship exhaust polluting emissions. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) for carbon dioxide sequestration. Certain embodiments may also be used to mitigate high acidity of SOx scrubber effluents, while some embodiments solve both issues (i.e., seawater acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely and permanently stored in the ocean.|CPC codes|(US20240350972 A1)|B01D-053/14/75|B01D-053/14/93|B01D-053/18|B01D-053/50/1|B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/92|B01D-2251/404|B01D-2251/606|B01D-2252/1035|B01D-2257/302|B01D-2257/504|B01D-2259/4566|(WO2024226673 A3)|B01D-053/14/75|B01D-053/14/93|B01D-053/18|B01D-053/50/1|B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/92|B01D-2251/404|B01D-2251/606|B01D-2252/1035|B01D-2257/302|B01D-2257/504|B01D-2259/4566|(AU2024264529 A1)|B01D-053/14/75|B01D-053/14/93|B01D-053/18|B01D-053/50/1|B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/92|B01D-2251/404|B01D-2251/606|B01D-2252/1035|B01D-2257/302|B01D-2257/504|B01D-2259/4566|(CN121605002 A)|B01D - 053/14/75 |B01D - 053/14/93 |B01D - 053/18 |B01D - 053/50/1 |B01D - 053/62 |B01D - 053/75 |B01D - 053/78 |B01D - 053/92 |B01D - 2251/404 |B01D - 2251/606 |B01D - 2252/1035 |B01D - 2257/302 |B01D - 2257/504 |B01D - 2259/4566 |(KR20260027884 A)|B01D-053/14/75|B01D-053/14/81|B01D-053/14/93|B01D-053/18|B01D-053/50/1|B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/92|B01D-2251/404|B01D-2251/606|B01D-2252/1035|B01D-2257/302|B01D-2257/504|B01D-2259/4566|(EP4705006 A2)|B01D-053/14/75|B01D-053/14/93|B01D-053/18|B01D-053/50/1|B01D-053/62|B01D-053/75|B01D-053/78|B01D-053/92|B01D-2251/404|B01D-2251/606|B01D-2252/1035|B01D-2257/302|B01D-2257/504|B01D-2259/4566|IPC codes|(US20240350972 A1)|B01D-053/14|B01D-053/18|B01D-053/50|B01D-053/62|B01D-053/75|B01D-053/78|(WO2024226673 A3)|B01D-053/34|B01D-053/46|B01D-053/62|B01D-053/73|(AU2024264529 A1)|B01D-053/34|B01D-053/46|B01D-053/62|B01D-053/73|(IN202517114935 A)|B01D-053/34|B01D-053/46|B01D-053/62|B01D-053/73|(CN121605002 A)|B01D - 053/34 |B01D - 053/46 |B01D - 053/62 |B01D - 053/73 |(KR20260027884 A)|B01D-053/14|B01D-053/18|B01D-053/62|B01D-053/78|(EP4705006 A2)|B01D-053/34|B01D-053/46|B01D-053/62|B01D-053/73| Environmental technology B01D-053/14/75|B01D-053/14/81|B01D-053/14/93|B01D-053/18|B01D-053/34/3|B01D-053/46|B01D-053/50/1|B01D-053/62|B01D-053/73|B01D-053/75|B01D-053/78|B01D-053/83|B01D-053/92|B01D-2251/304|B01D-2251/402|B01D-2251/404|B01D-2251/602|B01D-2251/604|B01D-2251/606|B01D-2252/1035|B01D-2257/302|B01D-2257/504|B01D-2258/0233|B01D-2258/0283|B01D-2259/4566|C01B-032/60|C01D-007/10|C01F-005/24|C04B-007/36/7|Y02A-050/2342|Y02C-010/04|Y02C-010/06|Y02C-010/08|Y02C-020/40|Y02E-020/326|Y02P-020/152 B01D-053/14/75|B01D-053/14/81|B01D-053/14/93|B01D-053/18|B01D-053/34/3|B01D-053/46|B01D-053/50/1|B01D-053/62|B01D-053/73|B01D-053/75|B01D-053/78|B01D-053/83|B01D-053/92|B01D-2251/304|B01D-2251/402|B01D-2251/404|B01D-2251/602|B01D-2251/604|B01D-2251/606|B01D-2252/1035|B01D-2257/302|B01D-2257/504|B01D-2258/0233|B01D-2258/0283|B01D-2259/4566|C01B-032/60|C01D-007/10|C01F-005/24|C04B-007/36/7|Y02A-050/2342|Y02C-010/04|Y02C-010/06|Y02C-010/08|Y02C-020/40|Y02E-020/326|Y02P-020/152 B01D-053/14|B01D-053/18|B01D-053/34|B01D-053/46|B01D-053/50|B01D-053/62|B01D-053/73|B01D-053/75|B01D-053/78 B01D-053/14|B01D-053/18|B01D-053/34|B01D-053/46|B01D-053/50|B01D-053/62|B01D-053/73|B01D-053/75|B01D-053/78 WO202606474 WO202606474 117087650 WHO=Examiner SELF=Y CAT=P CAT=/ CAT=X US20220259130|US20220096997|US20220203297|US20220048606|US20170001886 US20220259130 92883627 WHO=Examiner SELF=N CAT=Y|US20220096997 90361066 WHO=Examiner SELF=N CAT=Y|US20220203297 91335021 WHO=Examiner SELF=N CAT=A|US20220048606 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number=AU2024264529 (EP4705006)|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR|(EP4705006)|Extension States: BA|(EP4705006)|Validation States: MA, MD, TN, KH, GE|(WO2024/226673)|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW|(WO2024/226673)|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ|(WO2024/226673)|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR|(WO2024/226673)|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML|(WO2024/226673)|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (EP4705006)|EP|(US20240350972)|US|(WO2024/226673)|WO; AU; CN; EP; IN; JP; KR|(CN121605002)|CN|(KR10-2026-0027884)|KR|(IN202517114935)|IN|(AU2024264529)|AU https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=NLZ9hKgemAUyyWPhwc2q1W8tmrmn8uQzNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022297720&ekey=1772&xpn=EP4705006&kind=A2 https://register.epo.org/application?number=EP24797870 https://permalink.orbit.com/RenderStaticFirstPage?XPN=OP1xVE35ZgLWqxLm4QBXD3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT US (WO2024/226673)|US|(WO2024/226673)|US|(US20240350972)|US (WO2024/226673)|NAME=CALCAREA, INC. 448 S. Hill Street, Suite 515 Los Angeles, CA 90013 , COUNTRY=US|(WO2024/226673)|NAME=CALCAREA, INC. 448 S. Hill Street, Suite 515 Los Angeles, CA 90013 , COUNTRY=US|(US20240350972)|NAME=Calcarea, Inc. , CITY=Los Angeles , STATE=CA , COUNTRY=US , ATYP=US Company (EP4705006)|AT|(WO2024/226673)|US|(WO2024/226673)|US|||(AU2024264529)|AU (EP4705006)|NAME=Patentanwaltskanzlei Matschnig & Forsthuber OG;Biberstraße 22 Postfach 36 , CITY=1010 Wien , COUNTRY=AT , REG=101506908|(WO2024/226673)|NAME=PECK, John, W. KPPB LLP 3780 Kilroy Airport Way, Suite 320 Long Beach, CA 90806 , POSTCODE=90806 , COUNTRY=US|(WO2024/226673)|NAME=PECK, John, W. KPPB LLP 3780 Kilroy Airport Way, Suite 320 Long Beach, CA 90806 , POSTCODE=90806 , COUNTRY=US|(CN121605002)|NAME=ZHAO FANGXIAN;CCPIT PATENT AND TRADEMARK LAW OFFICE , REG=11038|(KR10-2026-0027884)|NAME=YOU ME PATENT & LAW FIRM|(AU2024264529)|NAME=Monks IP PO Box 164 , CITY=BLACKHEATH , STATE=NSW , POSTCODE=2785 , COUNTRY=AU (EP4705006)|US; US; US|(US20240350972)|US; US; US|(WO2024/226673)|US; US; US|(WO2024/226673)|US; US; US|(CN121605002)|US||| (EP4705006)|NAME=ADKINS, Jess, Firey, CITY=Altadena, CA 91001, COUNTRY=US |NAME=FORIN, Pierre, CITY=Los Angeles, CA 90013, COUNTRY=US |NAME=GUTIERREZ, Melissa, CITY=Los Angeles, CA 90013, COUNTRY=US|(US20240350972)|NAME=Adkins Jess Firey, CITY=Altadena, STATE=CA , COUNTRY=US |NAME=Forin Pierre, CITY=Los Angeles, STATE=CA , COUNTRY=US |NAME=Gutierrez Melissa, CITY=Los Angeles, STATE=CA , COUNTRY=US|(WO2024/226673)|NAME=ADKINS, Jess, Firey 1731 Morada Place Altadena, CA 91001, POSTCODE=91001, COUNTRY=US |NAME=FORIN, Pierre 448 S. Hill Street, Suite 515 Los Angeles, CA 90013, POSTCODE=90013, COUNTRY=US |NAME=GUTIERREZ, Melissa 448 S. Hill Street, Suite 515 Los Angeles, CA 90013, POSTCODE=90013, COUNTRY=US|(WO2024/226673)|NAME=ADKINS, Jess, Firey 1731 Morada Place Altadena, CA 91001, POSTCODE=91001, COUNTRY=US |NAME=FORIN, Pierre 448 S. Hill Street, Suite 515 Los Angeles, CA 90013, POSTCODE=90013, COUNTRY=US |NAME=GUTIERREZ, Melissa 448 S. Hill Street, Suite 515 Los Angeles, CA 90013, POSTCODE=90013, COUNTRY=US|(CN121605002)|NAME=J. F. Akins U.S.A., COUNTRY=US |NAME=Forin Philippe|NAME=M. Gutierrez|(KR10-2026-0027884)|NAME=ADKINS JESS FIREY|NAME=FORIN PIERRE|NAME=GUTIERREZ MELISSA|(IN202517114935)|NAME=Adkins Jess Firey|NAME=Forin Pierre|NAME=Gutierrez Melissa|(AU2024264529)|NAME=ADKINS, Jess, Firey|NAME=FORIN, Pierre|NAME=GUTIERREZ, Melissa 19 7 Titre: (EP4705006)|Ship based carbon capture, systems and methods of use thereof Résumé: (EP4705006)|Many embodiments are directed to reactors and methods for reducing ship exhaust polluting emissions. Many such embodiments are directed to reactors implementing accelerated weathering of limestone (AWL) for carbon dioxide sequestration. Certain embodiments may also be used to mitigate high acidity of SOx scrubber effluents, while some embodiments solve both issues (i.e., seawater acidification and carbon dioxide pollution). Many embodiments are implemented on cargo ships (e.g., container ships and/or bulk carriers) and use seawater. Certain embodiments can utilize effluent from one or more SOx scrubbers as the source of seawater to decarbonize and/or neutralize water prior to being safely and permanently stored in the ocean. 102 Abstract gpt-4o-mini yes The patent describes a method for carbon dioxide sequestration through accelerated weathering of limestone, which aligns with the topic of enhanced weathering for CO₂ capture.
109 CN202110483371 CN202110483371 CN113200545|CN113200545 95458395 CN113200545 B 2022-12-02 [CN113200545B]|CN113200545 A 2021-08-03 [CN113200545] 2021-04-30 2021-04-30 2022-12-02|2021-08-03 (CN113200545B)|2022-12-02 (CN113200545)|2041-04-30 (CN113200545)|Capacitance carbon and preparation method thereof (CN113200545)|The invention relates to capacitor carbon and a preparation method thereof. According to the main technical scheme, the preparation method of the capacitor carbon comprises the following steps: immersing a crushed and sieved biomass raw material into an additive solution for immersion treatment, and then drying the biomass raw material subjected to immersion treatment to obtain an additive-impregnated biomass raw material, the additive being a compound containing nitrogen and phosphorus; calcining the additive-impregnated biomass raw material impregnated in a protective atmosphere, raising the calcining temperature to 100-350 DEG C, preserving heat for a first set time, raising the calcining temperature to 400-1000 DEG C, and preserving heat for a second set time to obtain a calcined product; and washing and drying the calcined product to obtain the capacitor carbon. The four effects of carbon sequestration, carbonization, activation and doping are achieved through the calcination one-step method. The technology has the advantages that raw materials are low in price and easy to obtain, the technological process is short, the operation is easy, the cost is low, the yield is high, and the performance is good. Industrial production and commercial application of the capacitor carbon can be achieved easily. INSTITUTE OF COAL CHEMISTRY - CHINESE ACADEMY OF SCIENCE (CN113200545)|SHANXI INSTITUTE OF COAL CHEMISTRY CHINESE ACADEMY OF SCIENCES ([CN])|(CN113200545)|SHANXI INSTITUTE OF COAL CHEMISTRY CHINESE ACADEMY OF SCIENCES ([CN]) YUAN SHUXIA|ZHOU JINGJIE (CN113200545)|YUAN SHUXIA|ZHOU JINGJIE|(CN113200545)|YUAN SHUXIA|ZHOU JINGJIE (CN113200545)|LIANG YONGFANG;BEIJING XURUN LAW FIRM|Reg. Nb: 11522 (CN113200545)|Aiming at the problems, the invention provides a preparation technology which takes the agricultural and forestry waste biomass as a raw material and realizes four effects of carbon fixation, carbonization, activation and doping through a one-step method of dipping an additive and calcining; the preparation technology has the advantages of simple operation, short process flow and low cost, and can obtain the high-performance biomass-based capacitance carbon material doped with two N-P elements with high yield.|The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical solutions of the present invention more clearly understood and to implement them in accordance with the contents of the description, the following detailed description is given with reference to the preferred embodiments of the present invention and the accompanying drawings.| (CN113200545)|1. The preparation method of the capacitance carbon is characterized by comprising the following steps:and (3) dipping an additive: soaking the crushed and sieved biomass raw material into an additive solution for soaking treatment, and then drying the biomass raw material subjected to soaking treatment to obtain the biomass raw material impregnated with the additive; wherein the additive is a nitrogen and phosphorus containing compound; wherein, the additive is one or two of ammonium dihydrogen phosphate and diammonium hydrogen phosphate; the mass ratio of the biomass raw material to the additive in the additive solution is 1: (0.1-10); the biomass raw material is corn leaves or rice hulls;and (3) calcining: calcining the biomass raw material impregnated with the additive in a protective atmosphere, wherein the calcining temperature is firstly increased to 100-350 ℃, the temperature is maintained for a first set time, then the calcining temperature is increased to 400-1000 ℃, and the temperature is maintained for a second set time to obtain a calcined product; the first set time is 0.5-10h; the second set time is 0.5-10h;and (3) post-treatment: and washing and drying the calcined product to obtain the capacitance carbon.| (CN113200545)|The invention provides capacitance carbon and a preparation method thereof, and mainly aims to realize four effects of carbon fixation, carbonization, activation and doping through the steps of additive impregnation and calcination, thereby shortening the preparation process flow of the capacitance carbon, reducing the preparation cost and being beneficial to realizing the industrial production and the commercial application of biomass-based capacitance carbon. In order to achieve the above-mentioned object, the invention mainly provides the following technical scheme: in one aspect, an embodiment of the present invention provides a method for preparing capacitance carbon, where the method includes the following steps:|The invention relates to capacitance carbon and a preparation method thereof, which mainly adopts the technical scheme that: the preparation method of the capacitance carbon comprises the following steps: soaking the crushed and sieved biomass raw material into an additive solution for soaking treatment, and drying the biomass raw material subjected to soaking treatment to obtain the biomass raw material impregnated with the additive; the additive is a compound containing nitrogen and phosphorus; calcining the biomass raw material impregnated with the additive in a protective atmosphere, heating the calcining temperature to 100-350 ℃, preserving the heat for a first set time, heating the calcining temperature to 400-1000 ℃, and preserving the heat for a second set time to obtain a calcined product; and (4) washing and drying the calcined product to obtain the capacitance carbon.|The invention relates to the technical field of capacitance carbon, in particular to capacitance carbon and a preparation method thereof.| (CN113200545)|CAPACITANCE CARBON(100,61)|CRUSHED BIOMASS(98,3)|CARBON CAPACITY(70,25)|ADDITIVE(67,43)|FORESTRY WASTE BIOMASS(58,3)|CALCINATION PRODUCT(57,16)|SOAKING TREATMENT(54,3)|CALCINING TEMPERATURE(52,12)|ADDITIVE SOLUTION(44,15)|CAPACITIVE CARBON MESOPORE(44,1)|CALCINATION(39,21)|BIOMASS CAPACITANCE CARBON(38,3)|CARBONIZATION(35,7)|BIOMASS RAW MATERIAL(33,34)|BIOMASS FEEDSTOCK(33,4)|SIEVED BIOMASS RAW MATERIAL(32,3)|PHOSPHORUS(31,4)|PRODUCING CAPACITIVE CARBON(30,2)|CORN LEAVE(29,10)|CAPACITIVE CARBON YIELD(26,1)|MESH SIEVE(26,1)|PROTECTIVE ATMOSPHERE(25,6)|THEREFORE CAPACITIVE CARBON(22,10)|ADDITIVE IMPREGNATION(22,5)|ARGON ATMOSPHERE(22,2)|PREPARATION COST(22,1)|CARBON FIXATION(19,12)|DIPPING TREATMENT(19,4)|RICE HULL(19,4)|NITROGEN ATMOSPHERE(17,6)|CRUSHED CORN(15,5)|AMMONIUM DIHYDROGEN PHOSPHATE(15,4)|DIAMMONIUM HYDROGEN PHOSPHATE(14,18)|CRUSHED BIOMASS RAW MATERIAL(14,1)|INDUSTRIAL PRODUCTION(13,5)|POST TREATMENT(13,5)|DISCHARGE SPECIFIC CAPACITANCE(12,2)|DOPING MODIFICATION(11,4)|CAPACITANCE CARBON MESOPORE(11,2)|CAPACITANCE CARBON XPS SPECTRUM(11,2)|IMPREGNATION TREATMENT(10,4)|IMPREGNATION(10,3)|SIEVED CORN LEAF PARTICLE(10,1)|CAPACITANCE CARBON MATERIAL(8,4)|TUBULAR FURNACE(8,4)|DESORPTION ISOTHERM CURVE(8,1)|SUPERCAPACITOR ELECTROCHEMICAL PERFORMANCE(8,1)|CAPACITANCE CARBON YIELD(7,3)|FRUIT SHELL(7,2)|PHOSPHATE RADICAL(7,2)|TUBE FURNACE(7,2)|CAPACITANCE CARBON MICROPORE(7,1)|CAPACITANCE CARBON XRD SPECTRUM(7,1)|CAPACITIVE CARBON XRD SPECTRUM(7,1)|MASS RATIO(6,9)|CURRENT DENSITY(6,4)|CAPACITANCE CARBON COMMERCIAL APPLICATION(6,2)|ESTERIFICATION REACTION(6,2)|BIOMASS PRECURSOR(6,1)|CAPACITIVE CARBON XRD PATTERN(6,1)|CAPACITOR CARBON MESOPORE(6,1)|DIPPING ADDITIVE(6,1)|GREEN POLLUTION(6,1)|IMPREGNATION ADDITIVE(6,1)|N P(6,1)|SYNERGY THEORY(6,1)|THETHE CAPACITANCE CARBON(6,1)|SET TIME(5,14)|DIAMMONIUM HYDROGEN PHOSPHATE SOLUTION(5,7)|DEIONIZED WATER(5,6)|RAW MATERIAL(5,5)|ADSORPTION(5,3)|DIAMMONIUM PHOSPHATE SOLUTION(5,3)|SHORT PROCESS FLOW(5,3)|CAPACITOR CARBON CAPACITANCE(5,1)|CONP CONTENT(5,1)|ECONOMIC REQUIREMENT(5,1)|GRAPHITE MICROCRYSTAL CARBON LAYER(5,1)|IMPREGNATION MODIFICATION(5,1)|MACROMOLECULAR OXYGEN(5,1)|COMMERCIAL APPLICATION(4,6)|0F G(4,4)|CORN MASS RATIO(4,4)|CAPACITY CARBON(4,2)|HETEROATOM(4,2)|POROUS CARBON ELECTRODE(4,2)|REGULATION(4,2)|TAILING(4,2)|CAPACITANCE CARBON DISTRIBUTION(4,1)|CARBON CAPACITOR(4,1)|CRUSHING TREATMENT(4,1)|HYDRAZINE HYDRATE TREATMENT(4,1)|INTENSITY TENDENCY(4,1)|OLEFIN STRUCTURE POLYCONDENSATION(4,1)|PHYSICOCHEMICAL PROPERTY STABILITY(4,1)|PLASMA TREATMENT(4,1)|SEPARATION GROWTH(4,1)|SOLVOTHERMAL(4,1)||(CN113200545)|CAPACITANCE CARBON(100,74)|CRUSHED BIOMASS(88,3)|FORESTRY WASTE BIOMASS(71,4)|ADDITIVE(58,43)|SOAKING TREATMENT(48,3)|CARBON CAPACITY(45,19)|CALCINATION PRODUCT(38,12)|CALCINATION(36,19)|ADDITIVE SOLUTION(36,16)|BIOMASS CAPACITANCE CARBON(34,3)|CARBONIZATION(32,7)|CAPACITANCE CARBON MICROPORE(32,2)|BIOMASS FEEDSTOCK(30,4)|CALCINING TEMPERATURE(29,10)|CAPACITANCE CARBON MESOPORE(29,3)|SIEVED BIOMASS RAW MATERIAL(29,3)|PHOSPHORUS(28,4)|BIOMASS RAW MATERIAL(27,34)|PRODUCING CAPACITIVE CARBON(27,2)|CAPACITIVE CARBON YIELD(24,1)|MESH SIEVE(24,1)|PROTECTIVE ATMOSPHERE(23,6)|ADDITIVE IMPREGNATION(20,5)|FRUIT SHELL(20,3)|PREPARATION COST(20,1)|ARGON ATMOSPHERE(19,2)|CARBON FIXATION(17,12)|DIPPING TREATMENT(17,4)|NITROGEN ATMOSPHERE(16,6)|DISCHARGE SPECIFIC CAPACITANCE(16,4)|CRUSHED CORN(13,5)|MONOAMMONIUM PHOSPHATE(13,4)|CRUSHED BIOMASS RAW MATERIAL(13,1)|HEATING RATE(12,6)|RICE HULL(12,4)|SIEVED CORN LEAVE(12,3)|INDUSTRIAL PRODUCTION(11,5)|POST TREATMENT(11,5)|DOPING MODIFICATION(10,4)|STRAW(10,3)|CAPACITANCE CARBON2THE ADSORPTION(10,1)|IMPREGNATION TREATMENT(9,4)|IMPREGNATION(9,3)|300M2PER G(9,2)|CAPACITANCE CARBON XPS SPECTRUM(9,2)|SIEVED CORN LEAF PARTICLE(9,1)|CAPACITANCE CARBON MATERIAL(8,4)|CAPACITANCE CARBON YIELD(8,4)|TUBULAR FURNACE(8,4)|DESORPTION ISOTHERM CURVE(8,1)|SUPERCAPACITOR ELECTROCHEMICAL PERFORMANCE(8,1)|TUBE FURNACE(7,2)|CAPACITANCE CARBON XRD SPECTRUM(7,1)|CAPACITIVE CARBON XRD PROFILE(7,1)|CAPACITIVE CARBON XRD SPECTRUM(7,1)|SYNERGY THEORY(7,1)|DIBASIC AMMONIUM PHOSPHATE SOLUTION(6,12)|CURRENT DENSITY(6,4)|ADDITIVE DECOMPOSITION(6,1)|BIOMASS PRECURSOR(6,1)|CAPACITIVE CARBON XRD PATTERN(6,1)|CAPACITOR CARBON MESOPORE(6,1)|DIPPING ADDITIVE(6,1)|GREEN POLLUTION(6,1)|IMPREGNATION ADDITIVE(6,1)|N P(6,1)|DEIONIZED WATER(5,6)|HETEROATOM(5,3)|SHORT PROCESS FLOW(5,3)|400 1500M2PER G(5,2)|500 2000M2PER G(5,2)|CAPACITANCE CARBON COMMERCIAL APPLICATION(5,2)|ESTERIFICATION REACTION(5,2)|BIOCHAR YIELD(5,1)|CAPACITANCE CARBON XRD PATTERN(5,1)|CONP CONTENT(5,1)|ECONOMIC REQUIREMENT(5,1)|IMPREGNATION MODIFICATION(5,1)|MACROMOLECULAR OXYGEN(5,1)|RAW MATERIAL(4,5)|0F G(4,4)|CORN MASS RATIO(4,4)|SOAKING(4,4)|CARBON CAPACITOR(4,2)|POROUS CARBON ELECTRODE(4,2)|REGULATION(4,2)|TAILING(4,2)|CRUSHING TREATMENT(4,1)|HYDRAZINE HYDRATE TREATMENT(4,1)|INTENSITY TENDENCY(4,1)|OLEFIN STRUCTURE POLYCONDENSATION(4,1)|PHYSICOCHEMICAL PROPERTY STABILITY(4,1)|PLASMA TREATMENT(4,1)|SEPARATION GROWTH(4,1)|SGENERAL(4,1)|SOLVOTHERMAL(4,1)|COMMERCIAL APPLICATION(3,6)| (CN113200545)|1. The preparation method of the capacitance carbon is characterized by comprising the following steps:|and (3) dipping an additive: soaking the crushed and sieved biomass raw material into an additive solution for soaking treatment, and then drying the biomass raw material subjected to soaking treatment to obtain the biomass raw material impregnated with the additive; wherein the additive is a nitrogen and phosphorus containing compound; wherein, the additive is one or two of ammonium dihydrogen phosphate and diammonium hydrogen phosphate; the mass ratio of the biomass raw material to the additive in the additive solution is 1: (0.1-10); the biomass raw material is corn leaves or rice hulls;|and (3) calcining: calcining the biomass raw material impregnated with the additive in a protective atmosphere, wherein the calcining temperature is firstly increased to 100-350 ℃, the temperature is maintained for a first set time, then the calcining temperature is increased to 400-1000 ℃, and the temperature is maintained for a second set time to obtain a calcined product; the first set time is 0.5-10h; the second set time is 0.5-10h;|and (3) post-treatment: and washing and drying the calcined product to obtain the capacitance carbon.|2. The method of making capacitive carbon of claim 1, wherein in the step of impregnating an additive: the time of the dipping treatment is 0.5-12h.|3. The method of making capacitive carbon of claim 1, wherein the additive solution comprises an additive and water; wherein the amount of water is such that the additive solution will submerge the biomass feedstock during the impregnation process.|4. The method of making capacitive carbon of claim 1, wherein in the step of impregnating an additive: sieving the crushed biomass raw material through a 40-200 mesh sieve; and/or|Before the step of impregnating the additive, the method further comprises the following steps: and cleaning and drying the biomass raw material.|5. The method of making capacitive carbon of claim 1, wherein in the calcining step:|the calcination step is carried out in a tube furnace; and/or|The protective atmosphere is selected from a nitrogen atmosphere or an argon atmosphere; and/or|The heating rate is 0.1-20 ℃/min when the calcining temperature is increased to 100-350 ℃; and/or|The heating rate is 0.1-20 ℃/min when the temperature of the calcination is raised to 400-1000 ℃.|6. The method of producing capacitive carbon according to claim 1, wherein in the post-treatment step:|and washing the calcined product by using deionized water until the calcined product is neutral, and drying to obtain the capacitance carbon.|7. The method of producing capacitive carbon according to any one of claims 1 to 6, wherein the yield of capacitive carbon is 45 to 58%.|8. A capacitive carbon, characterized in that the capacitive carbon is prepared by the method for preparing the capacitive carbon according to any one of claims 1 to 7;|the capacitor carbon is doped with N element and P element, and has micropores smaller than 2nm and mesopores of 2-50 nm.|9. The capacitive carbon of claim 8 having a total specific surface area of 500-2000m 2 /g。|10. The capacitive carbon of claim 9 having a total specific surface area of 553.6-1629.6m 2 /g。|11. The capacitive carbon of claim 8 having a specific surface area of micropores of 400-1500m 2 /g。|12. The capacitive carbon of claim 11 having a micropore specific surface area of 473.5 to 1389.2m 2 /g。|13. The capacitive carbon of claim 8, wherein the specific surface area of the mesopore of the capacitive carbon is 50 to 300m 2 /g。|14. The capacitive carbon of claim 13 having a specific surface area of mesopores of 80.1 to 240.4m 2 /g。|15. The capacitive carbon according to claim 8, wherein the first discharge specific capacitance of the capacitive carbon is not less than 35.0F/g under the condition of an organic system and a current density of 50 mA/g; the specific capacitance of the capacitance carbon for the first time is more than or equal to 65.0F/g under the conditions of an inorganic system and a current density of 50 mA/g.|16. The capacitive carbon of claim 8 wherein the capacitive carbon has a relative content of N elements of 2-8% and a relative content of P elements of 1-4%.|17. The capacitive carbon of claim 16 wherein the capacitive carbon has a relative content of N element of 2.12-7.32% and a relative content of P element of 1.12-3.18%. (CN113200545)|TECHNICAL FIELD|[0001] The invention relates to the technical field of capacitance carbon, in particular to capacitance carbon and a preparation method thereof.|BACKGROUND ART|[0002] The super capacitor is also called as an electrochemical capacitor, is a novel green pollution-free energy storage device, has the characteristics of high charging and discharging speed, long service life, high power density, high energy conversion efficiency and the like, and has wide application prospects in the fields of electric automobiles, smart power grids, portable electronic equipment and the like. The super capacitor is mainly composed of components such as an electrode material, a diaphragm, electrolyte, a current collector and the like, wherein the electrode material is the key for determining the electrochemical performance of the super capacitor. In order to realize the commercial application of the electrode material, a preparation technology with short process route, low cost, high yield and good performance must be developed.|[0003] The biomass-based capacitance carbon material has the characteristics of good conductivity, large specific surface area, stable physicochemical properties, rich pore structure, cheap and easily available raw materials and the like, and becomes a research hotspot of the electrode material for the super capacitor.|[0004] At present, the conventional preparation method of biomass-based capacitance carbon material mainly comprises carbonization and activation treatment of biomass raw material, and also comprises a doping step in related technology, wherein common doping methods comprise a chemical vapor deposition method, a separation growth method, a solvothermal method, an arc discharge method, a heat treatment method, a plasma treatment method, a hydrazine hydrate treatment method and the like. However, each step in the conventional preparation method of the biomass-based capacitance carbon material needs to be performed step by step, so that the preparation process has long route, long operation flow and high cost.|[0005] Aiming at the problems, the invention provides a preparation technology which takes the agricultural and forestry waste biomass as a raw material and realizes four effects of carbon fixation, carbonization, activation and doping through a one-step method of dipping an additive and calcining; the preparation technology has the advantages of simple operation, short process flow and low cost, and can obtain the high-performance biomass-based capacitance carbon material doped with two N-P elements with high yield. The preparation technology is beneficial to realizing the industrial production and the commercial application of the capacitance carbon.|DISCLOSURE|Disclosure of Invention|[0006] The invention provides capacitance carbon and a preparation method thereof, and mainly aims to realize four effects of carbon fixation, carbonization, activation and doping through the steps of additive impregnation and calcination, thereby shortening the preparation process flow of the capacitance carbon, reducing the preparation cost and being beneficial to realizing the industrial production and the commercial application of biomass-based capacitance carbon.|[0007] In order to achieve the above-mentioned object, the invention mainly provides the following technical scheme:|[0008] in one aspect, an embodiment of the present invention provides a method for preparing capacitance carbon, where the method includes the following steps:|[0009] and (3) dipping an additive: soaking the crushed and sieved biomass raw material into an additive solution for soaking treatment, and then drying the biomass raw material subjected to soaking treatment to obtain the biomass raw material impregnated with the additive; wherein the additive is a nitrogen and phosphorus containing compound;|[0010] and (3) calcining: calcining the biomass raw material impregnated with the additive in a protective atmosphere, wherein the calcining temperature is firstly increased to 100-350 ℃, the temperature is maintained for a first set time, then the calcining temperature is increased to 400-1000 ℃, and the temperature is maintained for a second set time to obtain a calcined product;|[0011] and (3) post-treatment: and washing and drying the calcined product to obtain the capacitance carbon.|[0012] Preferably, in the step of impregnating with an additive: the additive is one or two of ammonium dihydrogen phosphate and diammonium hydrogen phosphate.|[0013] Preferably, in the step of impregnating with an additive: the mass ratio of the biomass raw material to the additive in the additive solution is 1: (0.1-10).|[0014] Preferably, the time of the impregnation treatment is 0.5 to 12 hours.|[0015] Preferably, the additive solution comprises an additive and water; wherein the amount of water is such that the additive solution will submerge the biomass feedstock during the impregnation process.|[0016] Preferably, in the step of impregnating with an additive: the biomass raw material after being crushed is sieved by a sieve with 40 to 200 meshes.|[0017] Preferably, before the step of impregnating the additive, the method further comprises: and cleaning and drying the biomass raw material.|[0018] Preferably, the biomass raw material is agricultural and forestry waste biomass, and any one of corn leaves, straws, rice hulls and fruit shells is preferably selected.|[0019] Preferably, in the calcining step:|[0020] the calcination step is carried out in a tube furnace; and/or|[0021] The protective atmosphere is selected from a nitrogen atmosphere or an argon atmosphere; and/or|[0022] The first set time is 0.5-10h; and/or|[0023] The heating rate is 0.1-20 ℃/min when the calcining temperature is heated to 100-350 ℃; and/or|[0024] The second set time is 0.5-10h; and/or|[0025] The heating rate is 0.1-20 ℃/min when the temperature is raised to 400-1000 ℃ during the calcination.|[0026] Preferably, in the post-treatment step: and washing the calcined product by using deionized water until the calcined product is neutral, and drying to obtain the capacitance carbon.|[0027] Preferably, the yield of the capacitance carbon is 45-58%.|[0028] On the other hand, the embodiment of the invention provides capacitance carbon, which is prepared by any one of the above capacitance carbon preparation methods; wherein, theThe capacitance carbon is doped with N element and P element, and the capacitance carbon has micropores less than 2nm and mesopores of 2-50 nm; preferably, the total specific surface area of the capacitance carbon is 500-2000m 2 Per g, preferably 553.6-1629.6m 2 (ii)/g; preferably, the specific surface area of micropores of the capacitance carbon is 400-1500m 2 /g, preferably 473.5-1389.2m 2 (iv) g; preferably, the specific surface area of the mesopores of the capacitance carbon is 50 to 300m 2 Per g, preferably from 80.1 to 240.4m 2 (ii)/g; preferably, the first discharge specific capacitance of the capacitance carbon is more than or equal to 35.0F/g under the conditions of an organic system and a current density of 50 mA/g; the specific capacitance of the capacitor carbon for the first discharge is more than or equal to 65.0F/g under the conditions of an inorganic system and the current density of 50 mA/g; preferably, the capacitance carbon has a relative content of N element of 2-8%, preferably 2.12-7.32%, and a relative content of P element of 1-4%, preferably 1.12-3.18%.|[0029] Compared with the prior art, the capacitance carbon and the preparation method thereof have the following beneficial effects:|[0030] on one hand, according to the preparation method of the capacitive carbon provided by the embodiment of the invention, the screened biomass raw material is subjected to impregnation treatment firstly, and then the impregnated biomass raw material is subjected to a set calcination treatment process, so that four effects of carbon fixation, carbonization, activation and doping are achieved by using a calcination one-step method, the yield of the biological carbon is improved, the regulation and control of a pore structure and a specific surface area and the doping modification of two kinds of hetero atoms N, P are completed, and the capacitive carbon (porous carbon electrode material) with low cost and excellent electrochemical performance is obtained. The invention realizes the preparation method of 'carbon fixation-carbonization-activation-doping' by a one-step method of impregnation and then calcination, greatly simplifies the process flow and is beneficial to realizing the industrial production and commercial application of the biomass-based capacitance carbon.|[0031] On the other hand, the capacitance carbon provided by the embodiment of the invention is prepared by the preparation method of the capacitance carbon, has larger specific surface area and better pore size distribution, is doped with N, P heteroatom, and has excellent electrochemical performance.|[0032] The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical solutions of the present invention more clearly understood and to implement them in accordance with the contents of the description, the following detailed description is given with reference to the preferred embodiments of the present invention and the accompanying drawings.|DRAWINGS DESCRIPTION|[0033] FIG. 1 is a flow chart of a method of making a capacitive carbon provided by an embodiment of the present invention;|[0034] FIG. 2 is an XRD spectrum of the capacitance carbon prepared in example 1 of the present invention and comparative example 1;|[0035] FIG. 3 shows N values of the capacitor carbon prepared in example 1 of the present invention and comparative example 1 2 Adsorption and desorption isothermal curves;|[0036] FIG. 4 is a pore size distribution diagram of the capacitance carbon prepared in example 1 of the present invention and comparative example 1;|[0037] FIG. 5 is an XPS spectrum of capacitance carbon prepared in example 1 of the present invention and comparative example 1;|[0038] fig. 6 is a specific capacity curve diagram of the capacitance carbon prepared in example 1 and comparative example 1 of the present invention.|INVENTION MODE|Detailed Description|[0039] To further explain the technical means and effects of the present invention adopted to achieve the predetermined object, the following detailed description of the embodiments, structures, features and effects according to the present invention will be made with reference to the accompanying drawings and preferred embodiments. In the following description, different "one embodiment" or "an embodiment" refers to not necessarily the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.|[0040] According to the invention, four effects of carbon fixation, carbonization, activation and doping are achieved by utilizing a calcination one-step method through the steps of firstly impregnating the additive solution and then carrying out a set calcination treatment process on the impregnated biomass raw material. The yield of the biochar is improved, and meanwhile, the regulation and control of a pore structure and a specific surface area and the doping modification of N, P heteroatom are completed, so that the capacitive carbon (porous carbon electrode material) with low cost and excellent electrochemical performance is obtained. The invention emphasizes that the preparation method of 'carbon fixation-carbonization-activation-doping' is realized by a one-step method of impregnation and then calcination, has low cost, short process flow and simple operation, and is beneficial to realizing the industrial production and commercial application of the biomass-based capacitance carbon.|[0041] The main process flow of the preparation method of the capacitance carbon provided by the embodiment of the invention is shown in figure 1, and mainly comprises the steps of impregnating an additive and calcining; the method comprises the following specific steps:|[0042] 1) The biomass feedstock is cleaned.|[0043] The biomass raw material of the invention is mainly agricultural and forestry waste biomass, preferably corn leaves, straws, rice hulls and fruit shells, but is not limited thereto.|[0044] 2) And (3) dipping an additive: and crushing and screening the cleaned biomass raw material, immersing the biomass raw material into an additive solution for impregnation, and drying the impregnated biomass raw material to obtain the biomass raw material impregnated with the additive.|[0045] Wherein, the additive is one or two of ammonium dihydrogen phosphate and diammonium hydrogen phosphate. The mass ratio of the biomass raw material to the additive in the additive solution is 1: (0.1-10). The time of the dipping treatment is 0.5-12h. The additive solution comprises an additive and water; wherein the amount of water is such that the additive solution will submerge the biomass feedstock during the impregnation process.|[0046] Here, it should be noted that: the mass ratio of the biomass material to the additive and the dipping time can be appropriately adjusted depending on the type of the biomass material and the type of the additive to be used. And setting the mass ratio of the biomass raw material to the additive in the additive solution as 1: (0.1-10), and further controlling the time of the dipping treatment to be 0.5-12h, so that the effects (such as carbon fixation, activation and doping) generated by the dipping additive can be achieved. Here, the impregnation mass ratio and the time of the impregnation treatment are set to the above ranges in view of the process requirement and the economic requirement.|[0047] Preferably, the biomass raw material after the crushing treatment passes through a sieve with 40-200 meshes. The selection of the particle size of the raw material is directly related to the impregnation treatment and the calcination process. Too small a particle size may result in a reduced char yield. Too large a particle size can result in too large a particle size of the final capacitive carbon product, resulting in a decrease in electrochemical performance.|[0048] 3) And (3) calcining: and calcining the biomass raw material impregnated with the additive in a protective atmosphere, wherein the calcining temperature is firstly increased to 100-350 ℃, the temperature is maintained for a first set time, then the calcining temperature is increased to 400-1000 ℃, and the temperature is maintained for a second set time to obtain a calcined product.|[0049] Wherein the first set time is 0.5-10h; the heating rate is 0.1-20 ℃/min when the calcining temperature is heated to 100-350 ℃.|[0050] The second set time is 0.5-10h; the heating rate is 0.1-20 ℃/min when the temperature is raised to 400-1000 ℃ during the calcination.|[0051] 4) And (3) post-treatment: and washing and drying the calcined product to obtain the capacitance carbon.|[0052] The theory of the synergy of the above steps, the step of impregnating the additive and the step of calcining, and how to achieve the four effects of carbon fixation, carbonization, activation and doping, of the present invention are described as follows:|[0053] the biomass raw material is impregnated, and then the biomass raw material impregnated with the additive is calcined at 100-350 ℃, so that the additive in the biomass raw material impregnated with the additive is heated and decomposed to generate phosphoric acid and ammonia gas. Wherein (1) phosphoric acid and biomass energy are subjected to esterification reaction, H atoms in the phosphoric acid are combined with-OH groups in the biomass to form water molecules to be removed, so that the catalytic action is generated in the chemical dehydration process of the biomass, the thermal decomposition process of the biomass is facilitated to be carried out towards the direction of generating solid carbon, more carbon atoms are left on the solid carbon skeleton instead of being carried out together with oxygen atoms by CO or CO 2 The form of the carbon dioxide is volatilized, or macromolecular oxygen-containing compounds, namely tar liquid substances, are generated, so that the purpose of carbon fixation is achieved. Meanwhile, the esterification reaction generates a phosphorus-containing compound, and phosphate radical is introduced into a biomass precursor to complete the doping of P; in the subsequent calcining temperature rise process of 400-1000 ℃, phosphate radicals have a barrier effect on the stacking process of the carbon microcrystals, so that the graphite-like microcrystal carbon layer is incomplete in development, is twisted or deformed to form defects, and further forms a pore structure in a sample, thereby forming a pore structure in carbonizationThe process of (2) completes the activation pore-forming at the same time. (2) The ammonia gas can promote the thermal polycondensation of olefin structure in biomass, is favorable for the generation of carbon microcrystal structure, and has the carbon fixing effect. Meanwhile, N element is introduced into the biomass structure, so that N doping is realized. In addition, the carbon fixation provided by the method mainly reduces the loss of carbon element, improves the yield and reduces the production cost.|[0054] The invention is further described below by means of specific examples:|[0055] example 1|[0056] The embodiment of the preparation of the capacitance carbon comprises the following specific preparation steps:|[0057] 1) Cleaning: cleaning and drying the biomass raw material corn leaves.|[0058] 2) Impregnation of an additive: crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. 10g of the sieved corn leaf particles are soaked in a diammonium hydrogen phosphate solution (wherein the mass ratio of the corn leaves to the diammonium hydrogen phosphate is 1:2; the water content in the diammonium hydrogen phosphate solution ensures that the diammonium hydrogen phosphate solution can submerge the corn leaves), stirred, soaked and treated for 6 hours, and then dried to obtain the corn leaves soaked with diammonium hydrogen phosphate.|[0059] 3) Calcining (carbon fixation-carbonization-activation-doping): putting the corn leaves soaked with diammonium hydrogen phosphate into a tubular furnace, and calcining in a nitrogen atmosphere; specifically, the temperature is increased to 200 ℃ at the heating rate of 2 ℃/min, the temperature is kept for 2h, then the temperature is increased to 700 ℃ at the heating rate of 2 ℃/min, and the temperature is kept for 1h. And cooling, taking out the calcined product, washing with deionized water to be neutral, and drying to obtain the capacitance carbon.|[0060] Example 2|[0061] This example prepared a capacitance carbon, and compared to example 1, the difference was step 2), and the other steps were identical. Wherein, step 2) of this embodiment is specifically as follows:|[0062] 2) Impregnation of an additive: crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. Taking 10g of sieved corn She Jinyu diammonium phosphate solution (wherein the mass ratio of corn leaves to diammonium phosphate is 1:0.1, and the water content in the diammonium phosphate solution ensures that the diammonium phosphate solution can immerse the corn leaves), stirring, dipping for 12 hours, and drying to obtain the corn leaves dipped with diammonium phosphate.|[0063] And other steps are consistent.|[0064] Example 3|[0065] In this example, a capacitance carbon was prepared, and compared with example 1, the preparation steps of this example are different in step 2), and the other steps are the same. Wherein, step 2) of this embodiment is specifically as follows:|[0066] 2) Impregnation of an additive: crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. Taking 10g of sieved corn She Jinyu diammonium hydrogen phosphate solution (wherein the mass ratio of corn leaves to diammonium hydrogen phosphate is 1.|[0067] And other steps are consistent.|[0068] Example 4|[0069] In this example, a capacitance carbon was prepared, and compared with example 1, the preparation steps of this example are different in step 2), and the other steps are the same. Wherein, step 2) of this embodiment is specifically as follows:|[0070] 2) Impregnation of an additive: crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. 10g of sieved corn She Jinyu diammonium hydrogen phosphate solution (wherein the mass ratio of corn leaves to diammonium hydrogen phosphate is 1:5, and the water content in the diammonium hydrogen phosphate solution ensures that the diammonium hydrogen phosphate solution can submerge the corn leaves), stirring, soaking and drying for 6 hours to obtain the corn leaves soaked with diammonium hydrogen phosphate.|[0071] The other steps are consistent.|[0072] Example 5|[0073] In this example, a capacitance carbon was prepared, and compared with example 1, the preparation steps of this example are different in step 3), and the other steps are the same. Wherein, step 3) of this embodiment is specifically as follows:|[0074] 3) And (3) calcining: putting the corn leaves soaked with diammonium hydrogen phosphate into a tubular furnace, and calcining in a nitrogen atmosphere; specifically, the temperature is raised to 350 ℃ at the heating rate of 2 ℃/min, the temperature is kept for 0.5h, then the temperature is raised to 1000 ℃ at the heating rate of 2 ℃/min, and the temperature is kept for 0.5h. And cooling, taking out the calcined product, washing with deionized water to be neutral, and drying to obtain the capacitance carbon.|[0075] Example 6|[0076] In this example, a capacitance carbon was prepared, and compared with example 1, the preparation steps of this example are different in step 3), and the other steps are the same. Wherein, step 3) of this embodiment is specifically as follows:|[0077] 3) And (3) calcining: putting the corn leaves impregnated with diammonium hydrogen phosphate into a tubular furnace, and calcining in a nitrogen atmosphere; specifically, the temperature is increased to 100 ℃ at the heating rate of 2 ℃/min, the temperature is kept for 10h, then the temperature is increased to 400 ℃ at the heating rate of 2 ℃/min, and the temperature is kept for 10h. And cooling, taking out the calcined product, washing with deionized water to be neutral, and drying to obtain the capacitance carbon.|[0078] Example 7|[0079] In this example, compared with example 1, in this example, in the step of dipping treatment, the additive solution adopted is ammonium dihydrogen phosphate, and other steps and process parameters are consistent|[0080] Example 8|[0081] This example is a capacitance carbon, and compared with example 1, the difference is that rice hulls are used as raw materials, and other preparation steps are consistent.|[0082] Comparative example 1|[0083] Comparative example 1 a capacitive carbon was prepared with the following specific steps:|[0084] 1) Cleaning and drying the corn leaves.|[0085] 2) Crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. 10g of sieved corn leaves are placed in a tubular furnace and calcined in nitrogen atmosphere; specifically, the temperature is increased to 200 ℃ at the heating rate of 2 ℃/min, the temperature is kept for 2h, then the temperature is increased to 700 ℃ at the heating rate of 2 ℃/min, and the temperature is kept for 1h. And cooling, taking out the calcined product, washing with deionized water to be neutral, and drying to obtain the capacitance carbon.|[0086] The capacitive carbons prepared in examples 1-8 and comparative example 1 were characterized by the following structures:|[0087] 1. the yields of the capacitance carbons prepared in examples 1 to 8 and comparative example 1 are shown in table 1.|[0088] TABLE 1|[0089] Capacitance carbonYield (%)Comparative example 126.5Example 145.9Example 245.0Example 358.0Example 453.7Example 548.6Example 654.9Example 747.2Example 851.4|[0090] As can be seen from Table 1, the yield of the capacitance carbon prepared in examples 1 to 8 of the present invention is greatly improved as compared with comparative example 1, and the purpose of expecting to improve the carbon yield is achieved.|[0091] 2. The XRD patterns of the capacitive carbon prepared in example 1 and comparative example 1 are shown in fig. 2.|[0092] Fig. 2 is an XRD spectrum of the capacitive carbon prepared in example 1 and comparative example 1. As can be seen from fig. 2: the XRD pattern of the capacitive carbon prepared in example 1 has a relatively sharp small angle (2 θ < 10 °), high intensity, and a tendency of intensity decrease with an increase in scanning angle, i.e., a "tailing" shape, which indicates that a certain amount of pore structure exists in the capacitive carbon prepared in example 1 of the present invention. The XRD profile of the capacitive carbon prepared in comparative example 1 also exhibited a certain "tailing" phenomenon, but was not very significant. It was shown that the capacitive carbon prepared in example 1 had a more developed pore structure than comparative example 1.|[0093] 3. N of capacitance carbon prepared in example 1 and comparative example 1 2 The adsorption and desorption isotherms are shown in FIG. 3.|[0094] As can be seen from FIG. 3, the method for preparing the capacity carbon according to example 1 of the present invention allows N of the capacity carbon to be increased through the step of impregnating the additive, as compared with comparative example 1 2 The adsorption and desorption amount is obviously increased, which shows that the capacitance carbon has larger specific surface area through impregnation modification, and the purpose of regulating and controlling the specific surface area is achieved.|[0095] 4. The specific surface areas of the total, micropores and mesopores of the capacitor carbons prepared in examples 1 to 8 and comparative example 1 are shown in Table 2.|[0096] TABLE 2|[0097] Sample (I)S General assembly (m 2 /g)S Micro-pores (m 2 /g)S Mesopores (m 2 /g)Comparative example 1201.5175.526.0Example 1596.7506.590.2Example 2553.6473.580.1Example 31629.61389.2240.4Example 41287.91065.8222.1Example 5816.5674.1142.4Example 6738.2602.1136.1Example 7693.7586.9106.8Example 8939.4802.1137.3|[0098] As can be seen from table 2: the total specific surface area of the capacitive carbon prepared in comparative example 1 was 201.5m 2 (g), the specific surface area of the carbon capacitors of examples 1 to 8 of the present invention was 553.6 to 1629.6m 2 The specific surface area of micropores (< 2 nm) and mesopores (2-50 nm) of the capacitance carbon prepared by the embodiment of the invention is increased, and the aim of increasing the specific surface area by activation is achieved.|[0099] 5. The pore size distribution of the capacitance carbon prepared in example 1 and comparative example 1 is shown in fig. 4.|[0100] As can be seen from fig. 4: according to the preparation method of the capacitance carbon provided by the embodiment of the invention, through the step of impregnating the additive, the number of micropores and mesopores of the capacitance carbon can be obviously increased, which shows that the impregnation additive achieves the purpose of optimizing the pore structure, and the result is consistent with the XRD characterization result.|[0101] The above shows that: the preparation method of the capacitance carbon provided by the embodiment of the invention can achieve the purpose of activating and pore-forming through the step of dipping the additive, so that the capacitance carbon has larger specific surface area and better pore size distribution, and is beneficial to improving the electrochemical performance.|[0102] 6. XPS spectra of the capacitance carbon prepared in example 1 and comparative example 1 are shown in fig. 5.|[0103] It can be seen from the XPS spectrum and the data in table 3 that the content of N, P element in the carbon materials prepared in examples 1-8 is much higher than the content of N, P element in the carbon material of comparative example 1, and the preparation scheme of the embodiment of the invention can realize the doping modification of N, P two kinds of hetero atoms, thereby achieving the design purpose of the doping modification of the invention.|[0104] Table 3 shows the comparison of the relative content of CONP in the capacitive carbon prepared in examples 1 to 8 and comparative example 1|[0105] TABLE 3|[0106] Sample (I)C(%)O(%)N(%)P(%)Comparative example 189.4610.480.040.02Example 185.574.896.712.83Example 292.373.362.421.85Example 385.114.567.323.01Example 487.233.136.882.76Example 595.331.012.121.54Example 680.2310.256.343.18Example 784.428.276.081.23Example 886.087.515.291.12|[0107] 7. FIG. 6 is a graph showing the specific capacity of the capacitor carbon prepared in example 1 and comparative example 1.|[0108] As can be seen from fig. 6: the discharge time of the capacitor carbon prepared in example 1 is longer than that of the capacitor carbon prepared in comparative example 1, which shows that the specific capacity of the capacitor carbon is increased and the electrochemical performance is improved by the step of impregnating the additive in the capacitor carbon preparation method provided by the embodiment of the invention.|[0109] The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and any simple modification, equivalent change and modification made to the above embodiment according to the technical spirit of the present invention are still within the scope of the technical solution of the present invention. (CN113200545)|TECHNICAL FIELD|[0001] The invention relates to the technical field of capacitance carbon, in particular to capacitance carbon and a preparation method thereof.|BACKGROUND ART|[0002] The super capacitor is also called as an electrochemical capacitor, is a novel green pollution-free energy storage device, has the characteristics of high charging and discharging speed, long service life, high power density, high energy conversion efficiency and the like, and has wide application prospects in the fields of electric automobiles, smart power grids, portable electronic equipment and the like. The super capacitor is mainly composed of components such as an electrode material, a diaphragm, electrolyte, a current collector and the like, wherein the electrode material is the key for determining the electrochemical performance of the super capacitor. In order to realize the commercial application of the electrode material, a preparation technology with short process route, low cost, high yield and good performance must be developed.|[0003] The biomass-based capacitance carbon material has the characteristics of good conductivity, large specific surface area, stable physicochemical properties, rich pore structure, cheap and easily available raw materials and the like, and becomes a research hotspot of the electrode material for the super capacitor.|[0004] At present, the conventional preparation method of biomass-based capacitance carbon material mainly comprises carbonization and activation treatment of biomass raw material, and also comprises a doping step in related technology, wherein common doping methods comprise a chemical vapor deposition method, a separation growth method, a solvothermal method, an arc discharge method, a heat treatment method, a plasma treatment method, a hydrazine hydrate treatment method and the like. However, each step in the conventional preparation method of the biomass-based capacitance carbon material needs to be performed step by step, so that the preparation process has long route, long operation flow and high cost.|[0005] Aiming at the problems, the invention provides a preparation technology which takes the agricultural and forestry waste biomass as a raw material and realizes four effects of carbon fixation, carbonization, activation and doping through a one-step method of dipping an additive and calcining; the preparation technology has the advantages of simple operation, short process flow and low cost, and can obtain the high-performance biomass-based capacitance carbon material doped with two N-P elements with high yield. The preparation technology is beneficial to realizing the industrial production and the commercial application of the capacitance carbon.|DISCLOSURE|Disclosure of Invention|[0006] The invention provides capacitance carbon and a preparation method thereof, and mainly aims to realize four effects of carbon fixation, carbonization, activation and doping through the steps of additive impregnation and calcination, thereby shortening the preparation process flow of the capacitance carbon, reducing the preparation cost and being beneficial to realizing the industrial production and the commercial application of biomass-based capacitance carbon.|[0007] In order to achieve the above-mentioned object, the invention mainly provides the following technical scheme:|[0008] in one aspect, an embodiment of the present invention provides a method for preparing capacitance carbon, where the method includes the following steps:|[0009] and (3) dipping an additive: soaking the crushed and sieved biomass raw material into an additive solution for soaking treatment, and then drying the biomass raw material subjected to soaking treatment to obtain the biomass raw material impregnated with the additive; wherein the additive is a nitrogen and phosphorus containing compound;|[0010] and (3) calcining: calcining the biomass raw material impregnated with the additive in a protective atmosphere, wherein the calcining temperature is firstly increased to 100-350 ℃, the temperature is maintained for a first set time, then the calcining temperature is increased to 400-1000 ℃, and the temperature is maintained for a second set time to obtain a calcined product;|[0011] and (3) post-treatment: and washing and drying the calcined product to obtain the capacitance carbon.|[0012] Preferably, in the step of impregnating with an additive: the additive is one or two of ammonium dihydrogen phosphate and diammonium hydrogen phosphate.|[0013] Preferably, in the step of impregnating with an additive: the mass ratio of the biomass raw material to the additive in the additive solution is 1: (0.1-10).|[0014] Preferably, the time of the impregnation treatment is 0.5 to 12 hours.|[0015] Preferably, the additive solution comprises an additive and water; wherein the amount of water is such that the additive solution will submerge the biomass feedstock during the impregnation process.|[0016] Preferably, in the step of impregnating with an additive: the biomass raw material after being crushed is sieved by a sieve with 40 to 200 meshes.|[0017] Preferably, before the step of impregnating the additive, the method further comprises: and cleaning and drying the biomass raw material.|[0018] Preferably, the biomass raw material is agricultural and forestry waste biomass, and any one of corn leaves, straws, rice hulls and fruit shells is preferably selected.|[0019] Preferably, in the calcining step:|[0020] the calcination step is carried out in a tube furnace; and/or|[0021] The protective atmosphere is selected from a nitrogen atmosphere or an argon atmosphere; and/or|[0022] The first set time is 0.5-10h; and/or|[0023] The heating rate is 0.1-20 ℃/min when the calcining temperature is heated to 100-350 ℃; and/or|[0024] The second set time is 0.5-10h; and/or|[0025] The heating rate is 0.1-20 ℃/min when the temperature is raised to 400-1000 ℃ during the calcination.|[0026] Preferably, in the post-treatment step: and washing the calcined product by using deionized water until the calcined product is neutral, and drying to obtain the capacitance carbon.|[0027] Preferably, the yield of the capacitance carbon is 45-58%.|[0028] On the other hand, the embodiment of the invention provides capacitance carbon, which is prepared by any one of the above capacitance carbon preparation methods; wherein, theThe capacitance carbon is doped with N element and P element, and the capacitance carbon has micropores less than 2nm and mesopores of 2-50 nm; preferably, the total specific surface area of the capacitance carbon is 500-2000m 2 Per g, preferably 553.6-1629.6m 2 (ii)/g; preferably, the specific surface area of micropores of the capacitance carbon is 400-1500m 2 /g, preferably 473.5-1389.2m 2 (iv) g; preferably, the specific surface area of the mesopores of the capacitance carbon is 50 to 300m 2 Per g, preferably from 80.1 to 240.4m 2 (ii)/g; preferably, the first discharge specific capacitance of the capacitance carbon is more than or equal to 35.0F/g under the conditions of an organic system and a current density of 50 mA/g; the specific capacitance of the capacitor carbon for the first discharge is more than or equal to 65.0F/g under the conditions of an inorganic system and the current density of 50 mA/g; preferably, the capacitance carbon has a relative content of N element of 2-8%, preferably 2.12-7.32%, and a relative content of P element of 1-4%, preferably 1.12-3.18%.|[0029] Compared with the prior art, the capacitance carbon and the preparation method thereof have the following beneficial effects:|[0030] on one hand, according to the preparation method of the capacitive carbon provided by the embodiment of the invention, the screened biomass raw material is subjected to impregnation treatment firstly, and then the impregnated biomass raw material is subjected to a set calcination treatment process, so that four effects of carbon fixation, carbonization, activation and doping are achieved by using a calcination one-step method, the yield of the biological carbon is improved, the regulation and control of a pore structure and a specific surface area and the doping modification of two kinds of hetero atoms N, P are completed, and the capacitive carbon (porous carbon electrode material) with low cost and excellent electrochemical performance is obtained. The invention realizes the preparation method of 'carbon fixation-carbonization-activation-doping' by a one-step method of impregnation and then calcination, greatly simplifies the process flow and is beneficial to realizing the industrial production and commercial application of the biomass-based capacitance carbon.|[0031] On the other hand, the capacitance carbon provided by the embodiment of the invention is prepared by the preparation method of the capacitance carbon, has larger specific surface area and better pore size distribution, is doped with N, P heteroatom, and has excellent electrochemical performance.|[0032] The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical solutions of the present invention more clearly understood and to implement them in accordance with the contents of the description, the following detailed description is given with reference to the preferred embodiments of the present invention and the accompanying drawings.|DRAWINGS DESCRIPTION|[0033] FIG. 1 is a flow chart of a method of making a capacitive carbon provided by an embodiment of the present invention;|[0034] FIG. 2 is an XRD spectrum of the capacitance carbon prepared in example 1 of the present invention and comparative example 1;|[0035] FIG. 3 shows N values of the capacitor carbon prepared in example 1 of the present invention and comparative example 1 2 Adsorption and desorption isothermal curves;|[0036] FIG. 4 is a pore size distribution diagram of the capacitance carbon prepared in example 1 of the present invention and comparative example 1;|[0037] FIG. 5 is an XPS spectrum of capacitance carbon prepared in example 1 of the present invention and comparative example 1;|[0038] fig. 6 is a specific capacity curve diagram of the capacitance carbon prepared in example 1 and comparative example 1 of the present invention.|INVENTION MODE|Detailed Description|[0039] To further explain the technical means and effects of the present invention adopted to achieve the predetermined object, the following detailed description of the embodiments, structures, features and effects according to the present invention will be made with reference to the accompanying drawings and preferred embodiments. In the following description, different "one embodiment" or "an embodiment" refers to not necessarily the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.|[0040] According to the invention, four effects of carbon fixation, carbonization, activation and doping are achieved by utilizing a calcination one-step method through the steps of firstly impregnating the additive solution and then carrying out a set calcination treatment process on the impregnated biomass raw material. The yield of the biochar is improved, and meanwhile, the regulation and control of a pore structure and a specific surface area and the doping modification of N, P heteroatom are completed, so that the capacitive carbon (porous carbon electrode material) with low cost and excellent electrochemical performance is obtained. The invention emphasizes that the preparation method of 'carbon fixation-carbonization-activation-doping' is realized by a one-step method of impregnation and then calcination, has low cost, short process flow and simple operation, and is beneficial to realizing the industrial production and commercial application of the biomass-based capacitance carbon.|[0041] The main process flow of the preparation method of the capacitance carbon provided by the embodiment of the invention is shown in figure 1, and mainly comprises the steps of impregnating an additive and calcining; the method comprises the following specific steps:|[0042] 1) The biomass feedstock is cleaned.|[0043] The biomass raw material of the invention is mainly agricultural and forestry waste biomass, preferably corn leaves, straws, rice hulls and fruit shells, but is not limited thereto.|[0044] 2) And (3) dipping an additive: and crushing and screening the cleaned biomass raw material, immersing the biomass raw material into an additive solution for impregnation, and drying the impregnated biomass raw material to obtain the biomass raw material impregnated with the additive.|[0045] Wherein, the additive is one or two of ammonium dihydrogen phosphate and diammonium hydrogen phosphate. The mass ratio of the biomass raw material to the additive in the additive solution is 1: (0.1-10). The time of the dipping treatment is 0.5-12h. The additive solution comprises an additive and water; wherein the amount of water is such that the additive solution will submerge the biomass feedstock during the impregnation process.|[0046] Here, it should be noted that: the mass ratio of the biomass material to the additive and the dipping time can be appropriately adjusted depending on the type of the biomass material and the type of the additive to be used. And setting the mass ratio of the biomass raw material to the additive in the additive solution as 1: (0.1-10), and further controlling the time of the dipping treatment to be 0.5-12h, so that the effects (such as carbon fixation, activation and doping) generated by the dipping additive can be achieved. Here, the impregnation mass ratio and the time of the impregnation treatment are set to the above ranges in view of the process requirement and the economic requirement.|[0047] Preferably, the biomass raw material after the crushing treatment passes through a sieve with 40-200 meshes. The selection of the particle size of the raw material is directly related to the impregnation treatment and the calcination process. Too small a particle size may result in a reduced char yield. Too large a particle size can result in too large a particle size of the final capacitive carbon product, resulting in a decrease in electrochemical performance.|[0048] 3) And (3) calcining: and calcining the biomass raw material impregnated with the additive in a protective atmosphere, wherein the calcining temperature is firstly increased to 100-350 ℃, the temperature is maintained for a first set time, then the calcining temperature is increased to 400-1000 ℃, and the temperature is maintained for a second set time to obtain a calcined product.|[0049] Wherein the first set time is 0.5-10h; the heating rate is 0.1-20 ℃/min when the calcining temperature is heated to 100-350 ℃.|[0050] The second set time is 0.5-10h; the heating rate is 0.1-20 ℃/min when the temperature is raised to 400-1000 ℃ during the calcination.|[0051] 4) And (3) post-treatment: and washing and drying the calcined product to obtain the capacitance carbon.|[0052] The theory of the synergy of the above steps, the step of impregnating the additive and the step of calcining, and how to achieve the four effects of carbon fixation, carbonization, activation and doping, of the present invention are described as follows:|[0053] the biomass raw material is impregnated, and then the biomass raw material impregnated with the additive is calcined at 100-350 ℃, so that the additive in the biomass raw material impregnated with the additive is heated and decomposed to generate phosphoric acid and ammonia gas. Wherein (1) phosphoric acid and biomass energy are subjected to esterification reaction, H atoms in the phosphoric acid are combined with-OH groups in the biomass to form water molecules to be removed, so that the catalytic action is generated in the chemical dehydration process of the biomass, the thermal decomposition process of the biomass is facilitated to be carried out towards the direction of generating solid carbon, more carbon atoms are left on the solid carbon skeleton instead of being carried out together with oxygen atoms by CO or CO 2 The form of the carbon dioxide is volatilized, or macromolecular oxygen-containing compounds, namely tar liquid substances, are generated, so that the purpose of carbon fixation is achieved. Meanwhile, the esterification reaction generates a phosphorus-containing compound, and phosphate radical is introduced into a biomass precursor to complete the doping of P; in the subsequent calcining temperature rise process of 400-1000 ℃, phosphate radicals have a barrier effect on the stacking process of the carbon microcrystals, so that the graphite-like microcrystal carbon layer is incomplete in development, is twisted or deformed to form defects, and further forms a pore structure in a sample, thereby forming a pore structure in carbonizationThe process of (2) completes the activation pore-forming at the same time. (2) The ammonia gas can promote the thermal polycondensation of olefin structure in biomass, is favorable for the generation of carbon microcrystal structure, and has the carbon fixing effect. Meanwhile, N element is introduced into the biomass structure, so that N doping is realized. In addition, the carbon fixation provided by the method mainly reduces the loss of carbon element, improves the yield and reduces the production cost.|[0054] The invention is further described below by means of specific examples:|[0055] example 1|[0056] The embodiment of the preparation of the capacitance carbon comprises the following specific preparation steps:|[0057] 1) Cleaning: cleaning and drying the biomass raw material corn leaves.|[0058] 2) Impregnation of an additive: crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. 10g of the sieved corn leaf particles are soaked in a diammonium hydrogen phosphate solution (wherein the mass ratio of the corn leaves to the diammonium hydrogen phosphate is 1:2; the water content in the diammonium hydrogen phosphate solution ensures that the diammonium hydrogen phosphate solution can submerge the corn leaves), stirred, soaked and treated for 6 hours, and then dried to obtain the corn leaves soaked with diammonium hydrogen phosphate.|[0059] 3) Calcining (carbon fixation-carbonization-activation-doping): putting the corn leaves soaked with diammonium hydrogen phosphate into a tubular furnace, and calcining in a nitrogen atmosphere; specifically, the temperature is increased to 200 ℃ at the heating rate of 2 ℃/min, the temperature is kept for 2h, then the temperature is increased to 700 ℃ at the heating rate of 2 ℃/min, and the temperature is kept for 1h. And cooling, taking out the calcined product, washing with deionized water to be neutral, and drying to obtain the capacitance carbon.|[0060] Example 2|[0061] This example prepared a capacitance carbon, and compared to example 1, the difference was step 2), and the other steps were identical. Wherein, step 2) of this embodiment is specifically as follows:|[0062] 2) Impregnation of an additive: crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. Taking 10g of sieved corn She Jinyu diammonium phosphate solution (wherein the mass ratio of corn leaves to diammonium phosphate is 1:0.1, and the water content in the diammonium phosphate solution ensures that the diammonium phosphate solution can immerse the corn leaves), stirring, dipping for 12 hours, and drying to obtain the corn leaves dipped with diammonium phosphate.|[0063] And other steps are consistent.|[0064] Example 3|[0065] In this example, a capacitance carbon was prepared, and compared with example 1, the preparation steps of this example are different in step 2), and the other steps are the same. Wherein, step 2) of this embodiment is specifically as follows:|[0066] 2) Impregnation of an additive: crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. Taking 10g of sieved corn She Jinyu diammonium hydrogen phosphate solution (wherein the mass ratio of corn leaves to diammonium hydrogen phosphate is 1.|[0067] And other steps are consistent.|[0068] Example 4|[0069] In this example, a capacitance carbon was prepared, and compared with example 1, the preparation steps of this example are different in step 2), and the other steps are the same. Wherein, step 2) of this embodiment is specifically as follows:|[0070] 2) Impregnation of an additive: crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. 10g of sieved corn She Jinyu diammonium hydrogen phosphate solution (wherein the mass ratio of corn leaves to diammonium hydrogen phosphate is 1:5, and the water content in the diammonium hydrogen phosphate solution ensures that the diammonium hydrogen phosphate solution can submerge the corn leaves), stirring, soaking and drying for 6 hours to obtain the corn leaves soaked with diammonium hydrogen phosphate.|[0071] The other steps are consistent.|[0072] Example 5|[0073] In this example, a capacitance carbon was prepared, and compared with example 1, the preparation steps of this example are different in step 3), and the other steps are the same. Wherein, step 3) of this embodiment is specifically as follows:|[0074] 3) And (3) calcining: putting the corn leaves soaked with diammonium hydrogen phosphate into a tubular furnace, and calcining in a nitrogen atmosphere; specifically, the temperature is raised to 350 ℃ at the heating rate of 2 ℃/min, the temperature is kept for 0.5h, then the temperature is raised to 1000 ℃ at the heating rate of 2 ℃/min, and the temperature is kept for 0.5h. And cooling, taking out the calcined product, washing with deionized water to be neutral, and drying to obtain the capacitance carbon.|[0075] Example 6|[0076] In this example, a capacitance carbon was prepared, and compared with example 1, the preparation steps of this example are different in step 3), and the other steps are the same. Wherein, step 3) of this embodiment is specifically as follows:|[0077] 3) And (3) calcining: putting the corn leaves impregnated with diammonium hydrogen phosphate into a tubular furnace, and calcining in a nitrogen atmosphere; specifically, the temperature is increased to 100 ℃ at the heating rate of 2 ℃/min, the temperature is kept for 10h, then the temperature is increased to 400 ℃ at the heating rate of 2 ℃/min, and the temperature is kept for 10h. And cooling, taking out the calcined product, washing with deionized water to be neutral, and drying to obtain the capacitance carbon.|[0078] Example 7|[0079] In this example, compared with example 1, in this example, in the step of dipping treatment, the additive solution adopted is ammonium dihydrogen phosphate, and other steps and process parameters are consistent|[0080] Example 8|[0081] This example is a capacitance carbon, and compared with example 1, the difference is that rice hulls are used as raw materials, and other preparation steps are consistent.|[0082] Comparative example 1|[0083] Comparative example 1 a capacitive carbon was prepared with the following specific steps:|[0084] 1) Cleaning and drying the corn leaves.|[0085] 2) Crushing the corn leaves cleaned in the step 1), and then sieving the crushed corn leaves with a 60-mesh sieve. 10g of sieved corn leaves are placed in a tubular furnace and calcined in nitrogen atmosphere; specifically, the temperature is increased to 200 ℃ at the heating rate of 2 ℃/min, the temperature is kept for 2h, then the temperature is increased to 700 ℃ at the heating rate of 2 ℃/min, and the temperature is kept for 1h. And cooling, taking out the calcined product, washing with deionized water to be neutral, and drying to obtain the capacitance carbon.|[0086] The capacitive carbons prepared in examples 1-8 and comparative example 1 were characterized by the following structures:|[0087] 1. the yields of the capacitance carbons prepared in examples 1 to 8 and comparative example 1 are shown in table 1.|[0088] TABLE 1|[0089] Capacitance carbonYield (%)Comparative example 126.5Example 145.9Example 245.0Example 358.0Example 453.7Example 548.6Example 654.9Example 747.2Example 851.4|[0090] As can be seen from Table 1, the yield of the capacitance carbon prepared in examples 1 to 8 of the present invention is greatly improved as compared with comparative example 1, and the purpose of expecting to improve the carbon yield is achieved.|[0091] 2. The XRD patterns of the capacitive carbon prepared in example 1 and comparative example 1 are shown in fig. 2.|[0092] Fig. 2 is an XRD spectrum of the capacitive carbon prepared in example 1 and comparative example 1. As can be seen from fig. 2: the XRD pattern of the capacitive carbon prepared in example 1 has a relatively sharp small angle (2 θ < 10 °), high intensity, and a tendency of intensity decrease with an increase in scanning angle, i.e., a "tailing" shape, which indicates that a certain amount of pore structure exists in the capacitive carbon prepared in example 1 of the present invention. The XRD profile of the capacitive carbon prepared in comparative example 1 also exhibited a certain "tailing" phenomenon, but was not very significant. It was shown that the capacitive carbon prepared in example 1 had a more developed pore structure than comparative example 1.|[0093] 3. N of capacitance carbon prepared in example 1 and comparative example 1 2 The adsorption and desorption isotherms are shown in FIG. 3.|[0094] As can be seen from FIG. 3, the method for preparing the capacity carbon according to example 1 of the present invention allows N of the capacity carbon to be increased through the step of impregnating the additive, as compared with comparative example 1 2 The adsorption and desorption amount is obviously increased, which shows that the capacitance carbon has larger specific surface area through impregnation modification, and the purpose of regulating and controlling the specific surface area is achieved.|[0095] 4. The specific surface areas of the total, micropores and mesopores of the capacitor carbons prepared in examples 1 to 8 and comparative example 1 are shown in Table 2.|[0096] TABLE 2|[0097] Sample (I)S General assembly (m 2 /g)S Micro-pores (m 2 /g)S Mesopores (m 2 /g)Comparative example 1201.5175.526.0Example 1596.7506.590.2Example 2553.6473.580.1Example 31629.61389.2240.4Example 41287.91065.8222.1Example 5816.5674.1142.4Example 6738.2602.1136.1Example 7693.7586.9106.8Example 8939.4802.1137.3|[0098] As can be seen from table 2: the total specific surface area of the capacitive carbon prepared in comparative example 1 was 201.5m 2 (g), the specific surface area of the carbon capacitors of examples 1 to 8 of the present invention was 553.6 to 1629.6m 2 The specific surface area of micropores (< 2 nm) and mesopores (2-50 nm) of the capacitance carbon prepared by the embodiment of the invention is increased, and the aim of increasing the specific surface area by activation is achieved.|[0099] 5. The pore size distribution of the capacitance carbon prepared in example 1 and comparative example 1 is shown in fig. 4.|[0100] As can be seen from fig. 4: according to the preparation method of the capacitance carbon provided by the embodiment of the invention, through the step of impregnating the additive, the number of micropores and mesopores of the capacitance carbon can be obviously increased, which shows that the impregnation additive achieves the purpose of optimizing the pore structure, and the result is consistent with the XRD characterization result.|[0101] The above shows that: the preparation method of the capacitance carbon provided by the embodiment of the invention can achieve the purpose of activating and pore-forming through the step of dipping the additive, so that the capacitance carbon has larger specific surface area and better pore size distribution, and is beneficial to improving the electrochemical performance.|[0102] 6. XPS spectra of the capacitance carbon prepared in example 1 and comparative example 1 are shown in fig. 5.|[0103] It can be seen from the XPS spectrum and the data in table 3 that the content of N, P element in the carbon materials prepared in examples 1-8 is much higher than the content of N, P element in the carbon material of comparative example 1, and the preparation scheme of the embodiment of the invention can realize the doping modification of N, P two kinds of hetero atoms, thereby achieving the design purpose of the doping modification of the invention.|[0104] Table 3 shows the comparison of the relative content of CONP in the capacitive carbon prepared in examples 1 to 8 and comparative example 1|[0105] TABLE 3|[0106] Sample (I)C(%)O(%)N(%)P(%)Comparative example 189.4610.480.040.02Example 185.574.896.712.83Example 292.373.362.421.85Example 385.114.567.323.01Example 487.233.136.882.76Example 595.331.012.121.54Example 680.2310.256.343.18Example 784.428.276.081.23Example 886.087.515.291.12|[0107] 7. FIG. 6 is a graph showing the specific capacity of the capacitor carbon prepared in example 1 and comparative example 1.|[0108] As can be seen from fig. 6: the discharge time of the capacitor carbon prepared in example 1 is longer than that of the capacitor carbon prepared in comparative example 1, which shows that the specific capacity of the capacitor carbon is increased and the electrochemical performance is improved by the step of impregnating the additive in the capacitor carbon preparation method provided by the embodiment of the invention.|[0109] The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and any simple modification, equivalent change and modification made to the above embodiment according to the technical spirit of the present invention are still within the scope of the technical solution of the present invention. Family Number|(95458395)|95458395|Abstract|(CN113200545B B)|The invention relates to capacitor carbon and a preparation method thereof . According to the main technical scheme , the preparation method of the capacitor carbon comprises the following steps : immersing a crushed and sieved biomass raw material into an additive solution for immersion treatment , and then drying the biomass raw material subjected to immersion treatment to obtain an additive - impregnated biomass raw material , the additive being a compound containing nitrogen and phosphorus ; calcining the additive - impregnated biomass raw material impregnated in a protective atmosphere , raising the calcining temperature to 100-350 DEG C , preserving heat for a first set time , raising the calcining temperature to 400-1000 DEG C , and preserving heat for a second set time to obtain a calcined product ; and washing and drying the calcined product to obtain the capacitor carbon . The four effects of carbon sequestration , carbonization , activation and doping are achieved through the calcination one - step method . The technology has the advantages that raw materials are low in price and easy to obtain , the technological process is short , the operation is easy , the cost is low , the yield is high , and the performance is good . Industrial production and commercial application of the capacitor carbon can be achieved easily . |CPC codes|(CN113200545B B)|C01B - 032/324 |C01B - 032/342 |IPC codes|(CN113200545B B)|C01B - 032/324 |C01B - 032/342 | Materials, metallurgy C01B-032/324|C01B-032/342|Y02E-060/13 C01B-032/324|C01B-032/342|Y02E-060/13 C01B-032/324|C01B-032/342 C01B-032/324|C01B-032/342 CN113880086|CN118702089|CN113479881|CN115651685B CN113880086 98008058 WHO=Examiner SELF=N CAT=Y|CN118702089 111611550 WHO=Examiner SELF=N CAT=X|CN113479881 96439409 WHO=Examiner SELF=Y CAT=T|CN115651685B 103658165 WHO=Examiner SELF=N CN103011155|CN101475165|CN112174136|CN111268675|CN110015662|CN109767927|CN109473291|CN109019554|CN108383119|CN108389728|CN102583311|CN101778794|US5102855|JP63069155|CN110858645|CN103771410 CN103011155 44859078 WHO=Examiner SELF=N CAT=Y|CN101475165 6770043 WHO=Examiner SELF=N CAT=Y|CN112174136 92171960 WHO=Examiner SELF=N CAT=A|CN111268675 89214482 WHO=Examiner SELF=N CAT=A|CN110015662 85377210 WHO=Examiner SELF=N CAT=A|CN109767927 84526135 WHO=Examiner SELF=N CAT=A|CN109473291 83723410 WHO=Examiner SELF=N CAT=A|CN109019554 82534847 WHO=Examiner SELF=N CAT=A|CN108383119 88785377 WHO=Examiner SELF=N CAT=A|CN108389728 80889807 WHO=Examiner SELF=N CAT=A|CN102583311 7788435 WHO=Examiner SELF=N CAT=A|CN101778794 1821343 WHO=Examiner SELF=N CAT=A|US5102855 421574 WHO=Examiner SELF=N CAT=A|JP63069155 23851770 WHO=Examiner SELF=N CAT=A|CN110858645 87751389 WHO=Examiner SELF=N|CN103771410 65423045 WHO=Examiner SELF=N HAN, JM ET AL.: &quot;High-Surface-Area Nitrogen/Phosphorus Dual-Doped Hierarchical Porous Carbon Derived from Biochar for Sulfur Holder&quot;, 《CHEMISTRYSELECT》 (Cat. A)|LI, M ET AL.: &quot;Removal of nitrogen and phosphorus pollutants from water by FeCl3-impregnated biochar&quot;, 《ECOLOGICAL ENGINEERING》 (Cat. A)|林晓强: &quot;生物质基多孔炭材料的制备及性能&quot;, 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 (Cat. A)|王茜: &quot;秸秆成型燃料提质及清洁燃烧特性研究&quot;, 《中国博士学位论文全文数据库 工程科技Ⅱ辑》 (Cat. A)|王振: &quot;炭基电极材料的制备及其表面性质对电化学性能的影响&quot;, 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 (Cat. A)|炭基电极材料的制备及其表面性质对电化学性能的影响;王振;《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》;20181015;全文 (Cat. A) JP63069155; US5102855; CN101475165; CN101778794; CN102583311; CN103011155; CN108383119; CN108389728; CN109019554; CN109473291; CN109767927; CN110015662; CN111268675; CN112174136; CN110858645; CN103771410 GRANTED (CN113200545)|GRANTED ALIVE (CN113200545)|ALIVE (CN113200545)|LEGAL DETAILS FOR CN113200545|Actual or expected expiration date=2041-04-30|Legal state=ALIVE|Status=GRANTED|Event publication date=2021-04-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202110483371|Application date=2021-04-30|Standardized application number=2021CN-0483371|Event publication date=2021-08-03|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN113200545|Publication stage code=A|Publication date=2021-08-03|Standardized publication number=CN113200545|Event publication date=2021-08-03|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2021-08-20|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2022-12-02|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN113200545|Publication stage code=B|Publication date=2022-12-02|Standardized publication number=CN113200545B|Event publication date=2022-12-02|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN113200545)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoThd/8h66eUmRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000065710691&ekey=2294&xpn=CN113200545B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=s6aABM%252FmS%252BFMoAS73c3v%252B7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN113200545)|CN|(CN113200545)|CN (CN113200545)|NAME=SHANXI INSTITUTE OF COAL CHEMISTRY CHINESE ACADEMY OF SCIENCES , COUNTRY=CN|(CN113200545)|NAME=SHANXI INSTITUTE OF COAL CHEMISTRY CHINESE ACADEMY OF SCIENCES , COUNTRY=CN (CN113200545)|NAME=LIANG YONGFANG;BEIJING XURUN LAW FIRM , REG=11522|(CN113200545)|NAME=LIANG YONGFANG;BEIJING XURUN LAW FIRM , REG=11522 (CN113200545)|NAME=YUAN SHUXIA|NAME=ZHOU JINGJIE|(CN113200545)|NAME=YUAN SHUXIA|NAME=ZHOU JINGJIE 0 1 Titre: (CN113200545)|Capacitance carbon and preparation method thereof Résumé: (CN113200545)|The invention relates to capacitor carbon and a preparation method thereof. According to the main technical scheme, the preparation method of the capacitor carbon comprises the following steps: immersing a crushed and sieved biomass raw material into an additive solution for immersion treatment, and then drying the biomass raw material subjected to immersion treatment to obtain an additive-impregnated biomass raw material, the additive being a compound containing nitrogen and phosphorus; calcining the additive-impregnated biomass raw material impregnated in a protective atmosphere, raising the calcining temperature to 100-350 DEG C, preserving heat for a first set time, raising the calcining temperature to 400-1000 DEG C, and preserving heat for a second set time to obtain a calcined product; and washing and drying the calcined product to obtain the capacitor carbon. The four effects of carbon sequestration, carbonization, activation and doping are achieved through the calcination one-step method. The technology has the advantages that raw materials are low in price and easy to obtain, the technological process is short, the operation is easy, the cost is low, the yield is high, and the performance is good. Industrial production and commercial application of the capacitor carbon can be achieved easily. 109 Abstract gpt-4o-mini no The article focuses on the preparation of capacitor carbon and its carbonization process, which does not relate to the accelerated weathering of minerals for CO₂ capture.
110 CN202511768705 CN202511768705 CN121426099 117637004 CN121426099 A 2026-01-30 [CN121426099] 2025-11-28 2025-11-28 2026-01-30 (CN121426099)|2045-11-28 (CN121426099)|Near-nano carbon-based material for recovering function and improving carbon fixation capacity of alien plant invasion damaged soil and preparation method thereof (CN121426099)|The invention discloses a near-nano carbon-based material for function recovery and carbon fixation capability improvement of alien plant invasion damaged soil and a preparation method of the near-nano carbon-based material, and belongs to the technical field of soil remediation and carbon fixation and sink increase. The near-nano carbon-based material is prepared by the following steps: by taking an external invasive plant Canadian yellow flower stalk as a raw material, crushing, screening, mixing with water, carrying out hydrothermal reaction to obtain a hydrothermal carbonization product, and carrying out ball milling and screening treatment to obtain the near-nano carbon-based material. The obtained near-nano carbon-based material has a high-aromaticity carbon skeleton, a rich mesoporous-macroporous structure and a relatively high amorphous silicon content, can efficiently adsorb and passivate residual allelochemicals of solidago canadensis, reconstruct an aggregate structure, promote microbial diversity and key enzyme activity recovery, strengthen organic carbon-mineral bonding and improve the stability of the material. Therefore, invasion-induced multifunctional soil degradation is accurately reversed, and in-situ remediation of the soil structure and function and improvement of the carbon immobilization capacity are achieved. Experimental results show that the carbon-based material provided by the invention can increase the multifunctional index of invasion-induced damaged soil by about 560% and increase the carbon sequestration index by about 48.1%. JIANGSU UNIVERSITY (CN121426099)|JIANGSU UNIVERSITY ([CN]) LI GUANLIN|ZHAO XIN|ZHANG QIUYUE|HU JIAN|WANG CHEN|LOU JIABAO|WANG YANJIAO|ZHENG XIAOJUN|CHEN XUNFENG|XIAO WENYA|DU DAOLIN (CN121426099)|LI GUANLIN|ZHAO XIN|ZHANG QIUYUE|HU JIAN|WANG CHEN|LOU JIABAO|WANG YANJIAO|ZHENG XIAOJUN|CHEN XUNFENG|XIAO WENYA|DU DAOLIN (CN121426099)|AN RAN;BEIJING SHENGGUANGXINHE IP FIRM|Reg. Nb: 16117 (CN121426099)|Compared with the prior art, the invention has the following advantages and technical effects:|Meanwhile, the method takes the solidago canadensis straw as the main raw material, realizes an ecological closed-loop path for intrusion treatment by using the waste biomass of the invasive plant through recycling, and has the advantages of easily available raw materials, environmental friendliness, controllable cost, large-scale application and the like.|The invention also provides the near-nano carbon-based material which is prepared by the preparation method and has the advantages of restoring the function of the soil caused by invasion of the foreign plant and improving the carbon-fixing capability.|However, the conventional carbon-based materials prepared by pyrolysis still have various limitations, such as large particles, limited specific surface area, insufficient dispersibility and limited surface functional groups, are difficult to penetrate into rhizosphere or aggregate micro-domain environments, lack the capability of specific action with chemosensory toxins, and are difficult to realize targeted restoration and carbon library stabilization enhancement of soil degradation caused by invasion of solidago canadensis.|In contrast, the SCB-HW4 carbon network prepared under the condition of 4 hours is not perfect, the stable carbon proportion is lower, and the carbon fixation index is improved only to a limited extent, while the SCB-HW12 prepared under the condition of 12 hours has higher aromaticity, but excessive polycondensation and pore degradation weaken the physical-chemical synergistic protection capability on soil organic carbon, so that the carbon fixation index is higher than that of the SCB-HW4 but still not as high as that of the SCB-HW.|When the ball milling time is only 2 hours, the grain diameter refinement degree is limited, the increase of the specific surface area and the surface active site is not obvious, the material still keeps more coarse grain structures, the rhizosphere and the aggregate micro-domain are difficult to fully enter, the adsorption and passivation capability of chemical sensing substances are limited, and the functional microorganisms are difficult to provide enough colonization sites, even certain disturbance is generated to the soil micro-environment due to the problems of unstable grain diameter distribution, local aggregation and the like, so that the multifunction is not effectively recovered.| (CN121426099)|1. The preparation method of the near-nano carbon-based material for restoring the function and improving the carbon-fixing capability of the damaged soil caused by invasion of the external plant is characterized by comprising the following steps of: (1) Crushing and sieving Canadian one-branch yellow flower stalks to obtain Canadian one-branch yellow flower stalk granules; (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water, and performing hydrothermal reaction to obtain a Canadian herba Solidaginis stalk hydrothermal carbonization product; (3) Ball milling is carried out on the solidago canadensis stalk hydrothermal carbonization product obtained in the step (2), and then sieving is carried out, so as to obtain the near-nano carbon-based material. | (CN121426099)|In order to achieve the above purpose, the present invention provides the following technical solutions: the invention provides a preparation method of a near-nano carbon-based material for restoring functions and improving carbon-fixing capacity of soil caused by invasion of foreign plants, wherein the foreign plants are solidago canadensis, and the preparation method comprises the following steps:|In order to solve the technical problems, the invention provides a near-nano carbon-based material for restoring the soil functions and improving the carbon-fixing capability caused by foreign plant invasion and a preparation method thereof.|The invention discloses a near-nano carbon-based material for restoring soil functions and improving carbon sequestration capacity due to foreign plant invasion and a preparation method thereof, belonging to the technical field of soil remediation and carbon sequestration and sequestration.| (CN121426099)|CARBON FIXATION(100,51)|NEAR NANO CARBON MATERIAL(100,33)|CARBON FIXATION CAPACITY(100,14)|FOREIGN PLANT INVASION(100,11)|FOREIGN PLANT(100,7)|RE SOIL FUNCTION(100,3)|CANADIAN HERBA SOLIDAGINIS STALK(87,4)|SOLIDAGO CANADENSIS STALK(66,4)|SOLIDAGO CANADENSIS(61,32)|SOLIDAGO CANADENSIS INVASION(60,10)|SOLIDAGO CANADENSIS STRAW(57,10)|PLANT INVASION(52,1)|CANADIAN HERBA(49,15)|INVASIVE PLANT WASTE BIOMASS(49,1)|CHEMOSENSORY TOXIN(48,1)|SOLIDAGINIS STALK PARTICLE(44,9)|CARBON LIBRARY STABILIZATION(41,1)|INSUFFICIENT DISPERSIBILITY(40,1)|SOLIDAGINIS STALK(39,4)|SOIL MICROENVIRONMENT(39,2)|CANADENSIS STALK(38,4)|WASTE BIOMASS(37,1)|INVASIVE PLANT SOLIDAGO(35,1)|CARBON FIXING CAPABILITY(33,3)|TARGETED RESTORATION(33,2)|ENOUGH COLONIZATION SITE(33,1)|INVASIVE DAMAGE SOIL(33,1)|CANADENSIS STRAW(32,12)|PORE DEGRADATION(32,1)|SOLIDIFIABLE SUBSTANCE(32,1)|RHIZOSPHERE(31,2)|AGGREGATE MICRO DOMAIN(31,1)|AGGREGATE MICRO DOMAIN ENVIRONMENT(31,1)|HYDROTHERMAL CARBONIZATION PRODUCTION(30,8)|SEQUESTRATION(29,1)|CARBON SEQUESTRATION CAPACITY(28,1)|FRIENDLINESS(28,1)|INTRUSION TREATMENT(28,1)|CARBON FIXATION INDEX(26,6)|DAMAGED SOIL(26,4)|MICROORGANISM FUNCTION(26,2)|PASSIVATION CAPABILITY(26,2)|BALL MILLING(24,58)|SCB HW(24,31)|HYDROTHERMAL CARBONIZED PRODUCT(24,3)|MICROORGANISM DIVERSITY(24,3)|PROTECTION CAPABILITY(24,1)|UNSTABLE GRAIN DIAMETER DISTRIBUTION(24,1)|MULTIFUNCTION(23,1)|SIEVING TREATMENT(23,1)|STABLE CARBON PROPORTION(23,1)|CANADIAN PARIS(22,3)|ACTION CAPABILITY(22,1)|AGGREGATION(22,1)|POLYCONDENSATION(21,2)|CONTROLLABLE COST(21,1)|FUNCTION RESTORATION(20,4)|AROMATICITY(20,2)|SOIL DEGRADATION(20,2)|SOIL REMEDIATION(20,2)|GRAIN DIAMETER(20,1)|SIEVING(18,7)|CARBON SEQUESTRATION(18,6)|INVASIVE PLANT(18,4)|SENSING SUBSTANCE(18,4)|AROMATIC CARBON SKELETON(18,1)|RICH MESOPOROUS MACROPOROUS STRUCTURE(18,1)|HYDROTHERMAL REACTION(17,27)|COLLECTING CANADIAN HERBA(17,4)|CARBON FIXING CAPACITY(16,3)|SOIL CARBON FIXING CAPACITY(16,2)|PYROLYSIS STILL(16,1)|GRANULE(15,3)|CARBON NETWORK(15,2)|CRUSHING(14,6)|ADSORPTION(14,4)|CARBON FIXATION ABILITY(14,3)|KEY ENZYME ACTIVITY RECOVERY(14,2)|RECYCLING(14,2)|AMORPHOUS SILICON CONTENT(14,1)|ECOLOGICAL CLOSED LOOP PATH(14,1)|GRAIN DIAMETER REFINEMENT DEGREE(14,1)|RE SOIL MULTIFUNCTIONALITY(13,2)|COARSE GRAIN STRUCTURE(12,1)|POTTING EXPERIMENT(11,5)|BALL MILLING EQUIPMENT(11,3)|AGGREGATE STRUCTURE(11,1)|LARGE PARTICLE(11,1)|MICRO ECOLOGY SYNERGISTIC RESTORATION(11,1)|PRETREATED SOLIDAGO CANADENSIS(11,1)|SOLIDAGO CANADENSIS BIOMASS WASTE(11,1)|SOLIDIFIABLE SOIL MULTIFUNCTIONAL RECOVERY(11,1)|STAINLESS STEEL BALL(10,7)|HYDROTHERMAL REACTION KETTLE(10,6)|SOIL VERSATILITY INDEX(10,3)|INVADED DAMAGED SOIL(10,2)|HOMOGENOUS GARDEN POT EXPERIMENT(10,1)|NANOSCALE REINFORCEMENT STABILIZATION(10,1)|POLLUTANT SYNERGISTIC PASSIVATION(10,1)|SOIL NUTRIENT CIRCULATION DISORDER(10,1)|DEIONIZED WATER(9,17)|HOMOLOGOUS INFLUENZA TOXIN(9,1)|MICROBIAL COMMUNITY DIVERSITY RECONSTRUCTION(9,1)|CARBON MATERIAL(8,47)|PLANETARY BALL MILL(8,11)|BALL MILLING SPEED(8,7)|SOIL CARBON FIXATION CAPACITY(8,6)|BALL STONE(8,4)|SOIL MICROPORE(8,3)|CANADIAN SOLIDAGO(8,2)|REALIZING RESTORATION(8,2)|CLOSED LOOP PATH(8,1)|EVEN CERTAIN DISTURBANCE(8,1)|LIMITED EXTENT(8,1)|MICROBIAL BIOMASS PHOSPHORUS(8,1)|RESIDUAL SOLIDAGO CANADENSIS(8,1)|SOIL MICROBIAL COMMUNITY RECONSTRUCTION(8,1)|SOIL VERSATILITY RESTORATION(8,1)|SOLANI LYRATI STALK PARTICLE(8,1)|AUTOGENOUS PRESSURE(7,8)|SOLID RESIDUE(7,8)|INVASION INDUCED DAMAGE SOIL(7,3)|ABSOLUTE ETHANOL(7,2)|BALL MASS RATIO(7,2)|EXOTIC PLANT SOLIDAGO(7,2)|SPARSE BONDING SITE(7,2)|STALK HYDROTHERMAL CARBONIZATION PRODUCT(7,2)|LIGNIN DEGRADATION FLORA(7,1)|MICROBIAL COMMUNITY DIVERSITY RECOVERY(7,1)|OPTIMIZING PORE CONNECTIVITY(7,1)|RE SOIL VERSATILITY(7,1)|RHIZOSPHERE MICRODOMAIN(7,1)|DISPERSIBILITY(6,4)|GROUND FUNCTION VARIABLE(6,3)|4000 MESH SIEVE(6,2)|ACTIVE SITE(6,2)|INVADING DAMAGE INDUCED SOIL(6,2)|PHENOLIC HYDROXYL(6,2)|RHIZOSPHERE ENVIRONMENT(6,2)|AMMONIA OXIDIZING BACTERIA(6,1)|BRANCH YELLOW STALK PARTICLE(6,1)|COLLECTING PEACH BRANCH PARTICLE(6,1)|CORN STALK PARTICLE(6,1)|DAMAGED SOIL AGGREGATE(6,1)|DEEP AROMATIZATION POLYCONDENSATION REACTION(6,1)|INDIGENOUS MICROORGANISM(6,1)|INTRUSION INDUCED SOIL VERSATILITY(6,1)|INVASION INDUCED SOIL VERSATILITY(6,1)|INVASIVE DAMAGED SOIL(6,1)|MICROBIAL BIOMASS NITROGEN(6,1)|MICROBIAL COLONIZATION SITE(6,1)|MICROECOLOGICAL IMBALANCE(6,1)|MIXING CANADIAN HERBA(6,1)|PASSIVATE POLLUTANT(6,1)|UNDERGROUND BIOMASS DISTRIBUTION(6,1)|SCB HW CARBON MATERIAL(5,12)|BALL MILLING TIME(5,9)|BALL MILLING MODIFICATION TREATMENT(5,5)|KEY PARAMETER(5,3)|SOIL ORGANIC CARBON(5,3)|SAMPLE INVESTIGATION(5,2)|SOIL CARBON RETENTION ABILITY(5,2)|AGRICULTURAL ENVIRONMENTAL SCIENCE JOURNAL(5,1)|AMORPHOUS SILICATE(5,1)|AROMATIC POLYCONDENSATION REACTION(5,1)|AVAILABLE RAW MATERIAL(5,1)|CARBON SEQUESTRATION SUSTAINABILITY(5,1)|CHEMOSENSORY SUBSTANCE(5,1)|CHINA FORESTRY(5,1)|COLLECTING CORN STRAW PARTICLE(5,1)|COLLECTING INVASION(5,1)|COMPREHENSIVE RECOVERY(5,1)|CORN STRAW CARBON AROMATICITY(5,1)|DIRECTIONAL EVOLUTION(5,1)|DURABLE CARBON WAREHOUSE(5,1)|EXOTIC INVASIVE PLANT(5,1)|EXPERIMENTAL FLOWERPOT(5,1)|EXTENSIVE REGULATION CAPABILITY(5,1)|FARMLAND SOIL(5,1)|HOMOLOGOUS SENSE SUBSTANCE INHIBITION(5,1)|INVADED SOIL(5,1)|INVASION SOIL TREATMENT(5,1)|INVASIVE SPECIES SOLIDAGO(5,1)|KEY SOIL FUNCTIONAL MICROORGANISM(5,1)|LIGNIN DERIVATIVE(5,1)|LIGNIN PROPORTION(5,1)|MATERIAL STILL(5,1)|MICROBIAL ATTACK(5,1)|MICROBIAL BIOMASS CARBON(5,1)|MICROORGANISM ADHESION(5,1)|MICROORGANISM IMBALANCE(5,1)|MODERATE HYDROPHOBICITY(5,1)|NANOSCALE INSULATION(5,1)|NEAR NANOSCALE CANADIAN GOLDENROD(5,1)|PHENOL SOLUBLE IMPURITY(5,1)|PORE COLLAPSE(5,1)|RESIDUAL ADSORPTION CAPACITY(5,1)|RESIDUAL ALLELOPATHY SUBSTANCE(5,1)|RESIDUAL BIOTOXICITY(5,1)|RESIDUAL HOMOLOGOUS SENSE SUBSTANCE(5,1)|SAMPLE SOIL MULTIFUNCTIONAL INDEX(5,1)|SOIL CARBON FIXATION SYNERGY(5,1)|SOIL MICROORGANISM FUNCTION(5,1)|SOIL PHYSICAL CHEMICAL ANALYSIS(5,1)|SOIL PHYSICOCHEMICAL PROPERTY IMPROVING(5,1)|SOIL RCP(5,1)|SOIL REFRACTORY CARBON LIBRARY(5,1)|SOLIDAGO CANADENSIS INVASION AREA(5,1)|SOLIDAGO STALK(5,1)|STRENGTHENING STABILIZATION(5,1)|TRIPLE OPTIMIZATION(5,1)|VEGETATION DEGRADATION(5,1)|VEGETATION DIVERSITY(5,1)|VERSATILITY RECOVERY(5,1)|SCB HN CARBON MATERIAL(4,8)|ABSOLUTE ETHYL ALCOHOL(4,3)|TABULAR DATA(4,3)|GROUND STRUCTURE DAMAGE(4,2)|HYDROTHERMAL CONDITION(4,2)|SILICON CARBON COMPOSITE SKELETON(4,2)|SOIL CARBON SEQUESTRATION ABILITY(4,2)|SOIL MATRIX(4,2)|SOIL PARTICLE(4,2)|VEGETATION COMMUNITY CHANGE(4,2)|ANTIDEGRADATION ORGANIC MINERAL(4,1)|BACTERIAL FUNGAL PROPORTION(4,1)|BIOMINERALIZATION LOSS(4,1)|CORE INNOVATION(4,1)|CORN STRAW COLLECTION(4,1)|CULTURE EXPERIMENT(4,1)|DOUBLE STABILIZATION(4,1)|EMBEDDING DOUBLE(4,1)|HOMOLOGOUS SUBSTANCE(4,1)|INVASION INDUCED SOIL CAPACITY(4,1)|LIGNIN CELLULOSE PROPORTION(4,1)|MICROBIAL HABITAT SPACE(4,1)|MICROORGANISM CARRIER(4,1)|MICROORGANISM HABITAT SPACE(4,1)|NATURAL ECOSYSTEM(4,1)|NYLON SIEVE(4,1)|PEACH TREE BRANCH(4,1)|PORE UNIFORMITY(4,1)|QUINONE PHENOL REDOX COUPLE(4,1)|REPAIR PRECISION(4,1)|RESIDUAL SENSING SUBSTANCE(4,1)|RESTORATION CAPACITY(4,1)|RICH PERCHING SPACE(4,1)|ROOT SECRETION(4,1)|SELF BIODEGRADATION RESISTANCE(4,1)|SOIL KEY ENZYME ACTIVITY(4,1)|STABILIZATION CAPABILITY(4,1)|TREATING INVASIVE DAMAGE(4,1)|Z SCORE STANDARDIZATION(4,1)|RAW MATERIAL(3,19)|PORE STRUCTURE(3,5)|SODIUM HYDROXIDE SOLUTION(3,5)|PI ACTION(3,4)|SCB HN ADDITION(3,4)|CARBON STABILITY(3,2)|INORGANIC COMPONENT(3,2)|MESOPOROUS MACROPOROUS HIERARCHIC STRUCTURE(3,2)|RHIZOSPHERE AREA(3,2)|SOIL CARBON FIXING ABILITY(3,2)|VENTILATION(3,2)|ACTIVATED ASH(3,1)|ALLELOCHEMICAL(3,1)|ARBUSCULAR MYCORRHIZAL FUNGUS(3,1)|AROMATIC CARBON NETWORK(3,1)|BIO DEGRADATION RESISTANCE(3,1)|BIOLOGICAL ACTIVITY INHIBITION(3,1)|BROKEN ROCK(3,1)|CARBON INDEX(3,1)|CARBON RETENTION CAPACITY(3,1)|CARBON SEQUESTRATION INDEX(3,1)|COMPETITIVENESS(3,1)|ENHANCEMENT CAPACITY(3,1)|GROUND SHIFT(3,1)|HYDROTHERMAL CARBONIZATION TEMPERATURE(3,1)|INSUFFICIENT DEVELOPMENT(3,1)|INVASIVE PLANT SUBSTANCE(3,1)|MBP INDEX(3,1)|MINERALIZATION RATE(3,1)|NANOSTRUCTURE(3,1)|NEAR NANOSCALE GRINDING(3,1)|PARTICLE BRIDGE(3,1)|PLASTIC FLOWERPOT(3,1)|PROLONGATION(3,1)|QUICK ACTING PHOSPHORUS(3,1)|RECOVERY FUNCTION(3,1)|REDUCING MIGRATION(3,1)|SAMPLE SOIL FUNCTIONAL VARIABLE(3,1)|SCB HN TREATMENT(3,1)|SCB HW TREATMENT(3,1)|SCB LW TREATMENT(3,1)|SILICEOUS COATING LAYER(3,1)| (CN121426099)|1. The preparation method of the near-nano carbon-based material for restoring the function and improving the carbon-fixing capability of the damaged soil caused by invasion of the external plant is characterized by comprising the following steps of:| (1) Crushing and sieving Canadian one-branch yellow flower stalks to obtain Canadian one-branch yellow flower stalk granules; | (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water, and performing hydrothermal reaction to obtain a Canadian herba Solidaginis stalk hydrothermal carbonization product; | (3) Ball milling is carried out on the solidago canadensis stalk hydrothermal carbonization product obtained in the step (2), and then sieving is carried out, so as to obtain the near-nano carbon-based material. |2. The method according to claim 1, wherein in the step (1), the particle size of the Canadian one-flower stalk particles is 180 to 250 μm.|3. The method of claim 1, wherein in step (2), the mass ratio of the canadian paris polyphylla stalk particles to deionized water is 1:10;| The temperature of the hydrothermal reaction is 260 ℃ and the time is 8 hours. |4. The method according to claim 1, wherein in the step (2), the step of filtering, washing and drying is further included after the completion of the hydrothermal reaction.|5. The method according to claim 4, wherein the washing is performed by alternately washing with deionized water and absolute ethanol, and then washing with a sodium hydroxide solution having a concentration of 0.1mol/L for 2-3 times.|6. The preparation method according to claim 1, wherein in the step (3), the ball mass ratio of the ball mill is 10:1, the ball milling speed is 500rpm, the ball milling time is 30min after 2-12h of ball milling, and the ball milling-rest process is repeated for 3 times.|7. The preparation method according to claim 1, wherein in the step (3), the ball milling equipment is a planetary ball mill, and the ball stone used for ball milling is stainless steel ball stone with the diameter of 10 mm.|8. The method according to claim 1, wherein in the step (3), the mesh number of the screen used for the sieving is 4000 mesh.|9. A near-nanocarbon-based material prepared by the preparation method according to any one of claims 1 to 8, which is characterized in that the function of soil is recovered and the carbon-fixing capacity is improved due to invasion of foreign plants.|10. Use of the near-nanocarbon-based material for improving the recovery of foreign plant invasion-induced soil function and the improvement of carbon fixation ability according to claim 9 for improving the recovery of foreign plant invasion-induced soil function and the improvement of carbon fixation ability. (CN121426099)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of soil remediation and carbon fixation and sink enhancement, and particularly relates to a near-nano carbon-based material for restoring functions and improving carbon fixation capacity of soil caused by invasion of foreign plants and a preparation method thereof.|BACKGROUND ART|[0002] Canadian Solidago (Solidago canadensis) is introduced into China since the 30 s of the 20 th century as a typical exotic invasive plant, and has spread to the east, south, middle and west areas of China, causing significant harm to farmlands and natural ecosystems. The species has strong competitiveness and is easy to form a single optimal community, so that the original local vegetation diversity is obviously reduced, the community structure is simplified and the underground biomass distribution is changed. The change of the vegetation community structure not only directly affects the composition of root secretions and the carbon flow input mode, but also indirectly drives the reconstruction of the soil microbial community by changing the rhizosphere environment. A large number of researches show that the solidago canadensis has obvious chemosensory effect in the invasion process, can continuously release phenolic acid, terpenoid and other chemosensory substances, and can inhibit the activity of key soil functional microorganisms (such as ammonia oxidizing bacteria, phosphate solubilizing bacteria, cellulose decomposing bacteria, arbuscular mycorrhizal fungi and the like), so that the diversity of the microorganisms is reduced, the community structure is abnormal and the nitrogen and phosphorus circulation function is weakened. Meanwhile, due to single vegetation community, reduced underground carbon source input and reduced quality after invasion, the bacterial/fungal proportion of soil shifts, so that lignin degradation flora is inhibited, and the formation of soil aggregates and the construction of a stable carbon reservoir (such as mineral bound organic carbon) are further affected. Thus, the invasion of solidago canadensis shows a chained effect of vegetation community change-rhizosphere environment change-microbial community change-ecological function degradation, and the superimposed toxin-sensing effect finally causes the soil structural damage, the acceleration of mineralization of organic matters and the degradation of carbon fixation capacity. In addition, even if the invasion of solidago canadensis is treated by methods such as manual pulling, cutting, burning, chemical prevention and control, the residual allelopathy substances cannot be eliminated, and the ecological functions of soil caused by vegetation degradation and microorganism imbalance cannot be recovered|[0003] Therefore, an effective treatment and restoration means for the damage soil caused by invasion of the exotic plant solidago canadensis is not available at present. The charcoal-based materials such as biochar have certain adsorption and soil physicochemical property improving effects, and are regarded as potential repairing materials. However, the conventional carbon-based materials prepared by pyrolysis still have various limitations, such as large particles, limited specific surface area, insufficient dispersibility and limited surface functional groups, are difficult to penetrate into rhizosphere or aggregate micro-domain environments, lack the capability of specific action with chemosensory toxins, and are difficult to realize targeted restoration and carbon library stabilization enhancement of soil degradation caused by invasion of solidago canadensis.|DISCLOSURE|Disclosure of Invention|[0004] In order to solve the technical problems, the invention provides a near-nano carbon-based material for restoring the soil functions and improving the carbon-fixing capability caused by foreign plant invasion and a preparation method thereof. Aiming at the problems of the loss of the function and the reduction of the carbon sink capacity of the invaded soil caused by the invasion of solidago canadensis, the near-nano carbon-based material prepared by the invention can effectively promote the reconstruction of the soil structure, the functional recovery and the enhancement of the formation capacity of a stable carbon reservoir, thereby simultaneously improving the soil multifunctionality and the carbon holding capacity. Meanwhile, the method takes the solidago canadensis straw as the main raw material, realizes an ecological closed-loop path for intrusion treatment by using the waste biomass of the invasive plant through recycling, and has the advantages of easily available raw materials, environmental friendliness, controllable cost, large-scale application and the like.|[0005] In order to achieve the above purpose, the present invention provides the following technical solutions:|[0006] the invention provides a preparation method of a near-nano carbon-based material for restoring functions and improving carbon-fixing capacity of soil caused by invasion of foreign plants, wherein the foreign plants are solidago canadensis, and the preparation method comprises the following steps: |[0007] (1) Crushing and sieving Canadian one-branch yellow flower stalks to obtain Canadian one-branch yellow flower stalk granules; |[0008] (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water, and performing hydrothermal reaction to obtain a Canadian herba Solidaginis stalk hydrothermal carbonization product; |[0009] (3) Ball milling is carried out on the solidago canadensis stalk hydrothermal carbonization product obtained in the step (2), and then sieving is carried out, so as to obtain the near-nano carbon-based material. |[0010] The invention is based on the ecological closed-loop concept of 'treating invasive damage with invasive organisms', and utilizes the characteristic that the solidago canadensis straw is rich in structural silicon and lignin derived aromatic carbon to directionally convert the solidago canadensis straw into near-nano carbon-based material, the silicon component can effectively deactivate homologous influenza toxin, and the high-aromaticity carbon skeleton cooperates with the nano structure to reconstruct soil aggregate, activate microorganism function and strengthen organic carbon-mineral bonding, thereby accurately reversing the degradation of the invasive induced soil function.|[0011] Further, in the step (1), the particle size of the Canadian one-branch yellow flower stalk particles is 180-250 μm.|[0012] Further, in the step (1), the mass ratio of the Canadian paris polyphylla stalk particles to the deionized water is 1:10.|[0013] Further, in the step (2), the hydrothermal reaction is performed under autogenous pressure, the temperature of the hydrothermal reaction is 260 ℃, and the time of the hydrothermal reaction is 8 hours. Further, in the step (2), the steps of filtering, washing and drying are further included after the hydrothermal reaction is finished.|[0014] Further, the washing process is to alternately wash with deionized water and absolute ethyl alcohol and then wash with sodium hydroxide solution with concentration of 0.1mol/L for 2-3 times.|[0015] Further, in the step (3), the ball material mass ratio of the ball milling is 10:1, the ball milling speed is 500rpm, the ball milling time is 30min after 2-12h of ball milling, and the ball milling-rest process is repeated for 3 times.|[0016] Further, in the step (3), the ball milling equipment is a planetary ball mill, and the ball stone used for ball milling is stainless steel ball stone with the diameter of 10 mm.|[0017] Further, in the step (3), the mesh number of the screen mesh used for the sieving is 4000 mesh.|[0018] The invention also provides the near-nano carbon-based material which is prepared by the preparation method and has the advantages of restoring the function of the soil caused by invasion of the foreign plant and improving the carbon-fixing capability.|[0019] The invention also provides application of the near-nano carbon-based material for improving the function recovery and carbon fixation capacity of the foreign plant invasion-induced damage soil in improving the function recovery and carbon fixation capacity of the foreign plant invasion-induced damage soil.|[0020] Compared with the prior art, the invention has the following advantages and technical effects:|[0021] (1) The near-nano carbon-based material prepared by the invention can realize the multifunctional recovery of the solidifiable soil caused by solidago canadensis and the improvement of the carbon fixation capacity. |[0022] (2) The invention optimizes the physical and chemical structure of the near-nano carbon-based material by controlling the temperature of the hydrothermal reaction, lays a foundation for in-situ restoration and carbon fixation synergy of soil, can remarkably improve the versatility of the soil, has the core mechanism that a developed mesoporous-macroporous hierarchical structure and a high specific surface area are formed by 260 ℃ hydrothermal carbonization (the specific surface area of the carbon-based material formed by 260 ℃ hydrothermal carbonization is 17.48m < 2 >/g, and the specific surface area of the carbon-based material formed by 180 ℃ hydrothermal carbonization is 3.10m < 2 >/g), enhances the adsorption capacity of the carbon-based material on the residual sensing substances of Solidago canadensis, effectively reduces the biotoxicity, and passivates pollutants in cooperation with mineral components such as silicon, potassium and the like in activated ash, promotes the diversity recovery of microbial communities, and systematically reverses the structural damage and the nutrient circulation disorder of the soil. The invention also improves the carbon fixation index of the near-nano carbon-based material by controlling the temperature of the hydrothermal reaction, which is derived from a stable carbon network formed by 260 ℃ hydrothermal carbonization deep aromatization polycondensation reaction, improves the self biodegradation resistance of the carbon-based material, and reduces migration and mineralization loss of active carbon components by pi-pi action or hydrogen bonding between the surface stable quinone groups and soil organic matters, thereby realizing long-acting carbon fixation.|[0023] (3) The soil multifunction value of the near-nano carbon-based material prepared by the invention is 475 percent higher than that of the carbon-based material (comparative example 2) prepared without ball milling modification treatment, and the near-nano carbon-based material has the advantages of huge specific surface area and high dispersibility caused by ultrafine particle size (near-nano grade), and the characteristics enable carbon particles to efficiently adsorb and passivate allelochemicals, penetrate into soil micropores and rhizosphere areas, provide exponentially growing microbial colonization sites, and meanwhile, compact network formed by particles bridge soil particles, enhance the stability of agglomerates, systematically improve physical structures such as ventilation, water holding and the like, and pertinently repair microecological imbalance caused by invasion. The carbon fixation index of the near-nano carbon-based material prepared by the method is 10% higher than that of the carbon-based material prepared without ball milling modification treatment, and the key mechanism is that nano-scale physical isolation and chemical bonding are double-action, ultrafine particles are embedded into the soil matrix (such as an aggregate or a mineral surface) to form a physical barrier to reduce the contact of organic carbon and microorganisms, and a large number of surface functional groups (such as carboxyl and phenolic hydroxyl) are exposed to be combined with organic matters strongly through coordination bonds or pi-pi action to form a stable organic-mineral-carbon complex, so that the long-term stability of a carbon warehouse is remarkably improved. Therefore, the near-nanoscale ball milling modification treatment serves as a core innovation point of the invention, and the repair precision and the carbon fixing efficiency of the carbon-based material are substantially enhanced through the size effect.|[0024] (4) The soil versatility of the near-nano carbon-based material prepared by utilizing the solidago canadensis is obviously higher than that of the near-nano carbon-based material prepared by utilizing corn stalks and peach branches, which is derived from the special ash composition (high potassium content) and pore structure of the raw materials, the amorphous silicate in the ash can effectively passivate homologous substances, and meanwhile, the developed mesopore-micropore system of the near-nano carbon-based material optimizes the water nutrient retention capacity, synergistically promotes the reconstruction of microbial activity, and realizes the targeted restoration of the invasive damaged soil. The carbon fixation index of the near-nano carbon-based material prepared by utilizing solidago canadensis is superior to that of the near-nano carbon-based material prepared by utilizing corn stalks and peach branches, and the core mechanism is a silicon-carbon composite skeleton with high silicon characteristics of raw materials and a surface quinone base derived from specific lignin proportion. The near-nano carbon-based material prepared by the method is used for fixing organic matters through chemical bonding (such as Si-O-C covalent bonding), so that a degradation-resistant complex is formed, and other raw materials (low aromaticity of corn straw carbon and sparse bonding sites of peach branch carbon) cannot provide equal-length stabilization protection. Therefore, the invasive species Solidago canadensis is taken as the raw material, so that the problem of difficult treatment of the Solidago canadensis biomass waste can be solved, the waste is used for recycling, and the pertinence of in-situ repair and the sustainability of carbon sequestration can be enhanced.|[0025] In conclusion, the method and the device cooperatively improve the in-situ restoration capacity and the carbon fixation and exchange enhancement capacity of the solidago canadensis induced damage farmland soil through triple optimization of the hydrothermal carbonization temperature (260 ℃), the particle size (near nano-scale) and the raw material (solidago canadensis), and provide an efficient and environment-friendly technical path for the invasion soil treatment.|DRAWINGS DESCRIPTION|[0026] The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention. In the drawings:|[0027] FIG. 1 is a graph showing the effect of adding the SCB-HN carbon-based material and the SCB-HW carbon-based material prepared in example 1 to soil on the versatility and carbon sequestration ability of the soil; |[0028] FIG. 2 is a graph showing the effect of adding the SCB-HN carbon-based material prepared in example 1, the CB-HN carbon-based material prepared in comparative example 4, and the PB-HN carbon-based material prepared in comparative example 5 to soil, on the versatility and carbon fixing ability of the soil. |INVENTION MODE|Detailed Description|[0029] The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0030] In order that the above-recited objects, features and advantages of the present invention will become more readily apparent, a more particular description of the invention will be rendered by reference to the appended drawings and appended detailed description.|[0031] The embodiment of the invention provides a preparation method of a near-nano carbon-based material with enhanced carbon-solid capacity and recovery of soil functions caused by invasion of solidago canadensis serving as an external plant, wherein the external plant is solidago canadensis, and the preparation method comprises the following steps:|[0032] (1) Crushing and sieving Canadian one-branch yellow flower stalks to obtain Canadian one-branch yellow flower stalk granules; |[0033] (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water, and performing hydrothermal reaction to obtain a Canadian herba Solidaginis stalk hydrothermal carbonization product; |[0034] (3) Ball milling is carried out on the solidago canadensis stalk hydrothermal carbonization product obtained in the step (2), and then sieving is carried out, so as to obtain the near-nano carbon-based material. |[0035] In a preferred embodiment, in the step (1), the step of washing and drying is further included before the crushing, and the drying temperature is 60 ℃. According to the invention, impurities such as soil on the surface of the solidago canadensis stalks are removed by cleaning.|[0036] In a preferred embodiment, in step (1), the sieving is a 60 mesh sieve.|[0037] In a preferred embodiment, in step (1), the particle size of the Canadian one-branch yellow flower stalk particles is 180-250 μm.|[0038] In a preferred embodiment, in the step (2), the mass ratio of the Canadian paris polyphylla stalk particles to deionized water is 1:10.|[0039] In a preferred embodiment, in step (2), the hydrothermal reaction is carried out under autogenous pressure, the temperature of the hydrothermal reaction is 260 ℃, and the time of the hydrothermal reaction is 8 hours.|[0040] In a preferred embodiment, in step (2), the hydrothermal reaction further comprises the steps of filtering, washing and drying after the completion of the hydrothermal reaction.|[0041] In a preferred embodiment, the washing is performed by first alternately washing with deionized water and absolute ethanol, and then washing 2-3 times with sodium hydroxide solution having a concentration of 0.1 mol/L. The purpose of the invention is to remove acid and phenol soluble impurities, activate oxygen-containing functional groups on the surface of the carbon, improve the purity, dispersibility and specific surface area of the material, and enhance the adsorption, chemical substance passivation and mineral binding capacity of the material, thereby remarkably improving the repairing and carbon fixing effects.|[0042] In a preferred embodiment, in the step (3), the ball mass ratio of the ball milling is 10:1, the ball milling speed is 500rpm, the ball milling time is 2-12h, and then the ball milling is stopped for 30min, the ball milling-stopping process is repeated for 3 times, and more preferably the ball milling time is 6h.|[0043] In a preferred embodiment, in the step (3), the ball milling equipment is a planetary ball mill, and the ball stone used for ball milling is stainless steel ball stone with the diameter of 10 mm.|[0044] In a preferred embodiment, in step (3), the mesh size of the screen used for the sieving is 4000 mesh.|[0045] The invention provides a near-nano carbon-based material which is prepared by the preparation method and is prepared from exotic plants, namely solidifiable by carbon and is improved in the function recovery and carbon fixation capacity of damaged soil caused by invasion of solidago canadensis.|[0046] The invention also provides application of the near-nano carbon-based material for improving the function recovery and carbon fixation capacity of the exotic plant solidago canadensis invasion-induced damage soil in improving the function recovery and carbon fixation capacity of the exotic plant invasion-induced damage soil.|[0047] In the examples of the present invention, room temperature refers to "25.+ -. 2 ℃.|[0048] Unless otherwise specified, the starting materials in the examples of the present invention were all obtained by commercial purchase.|[0049] Example 1|[0050] A preparation method of a near-nano carbon-based material for restoring functions and improving carbon-fixing capacity of soil caused by invasion of foreign plants comprises the following specific steps:|[0051] (1) Collecting Canadian herba Solidaginis stalks, cleaning surface impurities, drying at 60 ℃, pulverizing, sieving with 60 mesh sieve, and collecting Canadian herba Solidaginis stalk particles with particle size of 180-250 μm; |[0052] (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring the mixture into a hydrothermal reaction kettle, heating the mixture to 260 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 260 ℃ and autogenous pressure, cooling the mixture to room temperature, and filtering the mixture to obtain a solid residue; |[0053] (3) Transferring the canadian solidago stalk hydrothermal carbonized product obtained in the step (2) into a planetary ball mill, wherein the ball stones in the planetary ball mill are stainless steel ball stones with the diameter of 10mm, the ball material mass ratio is 10:1, the ball milling speed is 500rpm, the ball milling is carried out for 6 hours, the ball milling is carried out for 30 minutes, the ball milling-rest process is repeated for 3 times, and then the materials pass through a 4000-mesh sieve to obtain the near-nanoscale canadian solidago stalk carbon-based material which is marked as SCB-HN. |[0054] Comparative example 1|[0055] The difference from example 1 is that the temperature of the hydrothermal reaction is 180 ℃ and the ball milling modification treatment is not carried out, and the specific steps are as follows:|[0056] (1) Collecting Canadian herba Solidaginis stalks, cleaning surface impurities, drying at 60 ℃, pulverizing, sieving with 60 mesh sieve, and collecting Canadian herba Solidaginis stalk particles with particle size of 180-250 μm; |[0057] (2) Mixing Canadian herba Solani Lyrati stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring into a hydrothermal reaction kettle, heating to 180 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 180 ℃ and autogenous pressure, cooling to room temperature, filtering to obtain a solid residue, alternately cleaning the obtained solid residue with deionized water and absolute ethyl alcohol, then washing for 2 times with a sodium hydroxide solution with a concentration of 0.1mol/L, vacuum drying, and sieving with a 500-mesh sieve to obtain a Canadian herba Solani Lyrati stalk hydrothermal carbonization product, which is marked as SCB-LW. |[0058] Comparative example 2|[0059] The only difference from example 1 is that the time of hydrothermal reaction was changed without ball milling modification treatment, and the specific steps were as follows:|[0060] (1) Collecting Canadian herba Solidaginis stalks, cleaning surface impurities, drying at 60 ℃, pulverizing, sieving with 60 mesh sieve, and collecting Canadian herba Solidaginis stalk particles with particle size of 180-250 μm; |[0061] (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring into a hydrothermal reaction kettle, heating to 260 ℃, respectively carrying out hydrothermal reaction for 4h and 12h under the conditions of 260 ℃ and autogenous pressure, cooling to room temperature, filtering to obtain a solid residue, alternately cleaning the obtained solid residue with deionized water and absolute ethyl alcohol, then washing for 2 times with a sodium hydroxide solution with a concentration of 0.1mol/L, and carrying out vacuum drying to obtain Canadian herba Solidaginis stalk hydrothermal carbonization products which are respectively marked as SCB-HW4 and SCB-HW12. |[0062] Comparative example 3|[0063] The difference from example 1 is that the ball milling modification treatment time is respectively 2h and 12h, and the specific steps are as follows:|[0064] (1) Collecting Canadian herba Solidaginis stalks, cleaning surface impurities, drying at 60 ℃, pulverizing, sieving with 60 mesh sieve, and collecting Canadian herba Solidaginis stalk particles with particle size of 180-250 μm; |[0065] (2) Mixing the Canadian herba Solani first-branch yellow stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring the mixture into a hydrothermal reaction kettle, heating the mixture to 260 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 260 ℃ and autogenous pressure, cooling the mixture to room temperature, and filtering the mixture to obtain a solid residue; |[0066] (3) Transferring the Canadian goldenrod stalk hydrothermal carbonization product obtained in the step (2) into a planetary ball mill, wherein the ball stones in the planetary ball mill are stainless steel ball stones with the diameter of 10mm, the ball material mass ratio is 10:1, the ball milling speed is 500rpm, the ball milling is respectively carried out for 2 hours and 12 hours, then the ball milling is carried out for rest for 30 minutes, the ball milling-rest process is repeated for 3 times, and then the materials pass through a 4000-mesh sieve to obtain near-nanoscale Canadian goldenrod stalk carbon-based materials which are respectively marked as SCB-HN2 and SCB-HN12. |[0067] Comparative example 4|[0068] The difference with example 1 is that the solidago canadensis straw is replaced by corn straw to prepare the near-nanoscale corn straw carbon-based material, which comprises the following specific steps:|[0069] (1) Collecting corn straw, cleaning surface impurities, drying at 60 ℃, crushing, sieving with a 60-mesh sieve, and collecting corn straw particles with the particle size of 180-250 mu m; |[0070] (2) Mixing the corn stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring the mixture into a hydrothermal reaction kettle, heating the mixture to 260 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 260 ℃ and autogenous pressure, cooling the mixture to room temperature, and filtering the mixture to obtain a solid residue; |[0071] (3) Transferring the corn stalk hydrothermal carbonized product obtained in the step (2) into a planetary ball mill, wherein the ball stones in the planetary ball mill are stainless steel ball stones with the diameter of 10mm, the ball material mass ratio is 10:1, the ball milling speed is 500rpm, the ball milling is carried out for 6 hours, the rest is carried out for 30 minutes, the ball milling-rest process is repeated for 3 times, and then the corn stalk carbon-based material with the near nano-grade is obtained through a 4000-mesh sieve and is recorded as CB-HN. |[0072] Comparative example 5|[0073] The difference with example 1 is that the solidago canadensis straw is replaced by peach branches, and the preparation method of the near-nanoscale peach branch carbon-based material comprises the following specific steps:|[0074] (1) Collecting peach branches, cleaning surface impurities, drying at 60 ℃, crushing, sieving with a 60-mesh sieve, and collecting peach branch particles with the particle size of 180-250 mu m; |[0075] (2) Mixing the peach branch particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring the mixture into a hydrothermal reaction kettle, heating the mixture to 260 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 260 ℃ and autogenous pressure, cooling the mixture to room temperature, and filtering the mixture to obtain a solid residue; |[0076] (3) Transferring the peach tree branch hydrothermal carbonization product obtained in the step (2) into a planetary ball mill, wherein the ball stones in the planetary ball mill are stainless steel ball stones with the diameter of 10mm, the ball material mass ratio is 10:1, the ball milling speed is 500rpm, the ball milling is carried out for 6 hours, the rest is carried out for 30 minutes, the ball milling-rest process is repeated for 3 times, and then the peach tree branch charcoal base material with near nano-scale is obtained through a 4000-mesh sieve and is recorded as PB-HN. |[0077] Effect example 1|[0078] The carbon-based material (SCB-HW) prepared in the step (2) of the example 1 and the carbon-based material (SCB-LW) prepared in the comparative example 1 were analyzed for the improvement of the multi-functional recovery and carbon retention ability of the soil caused by the invasion of solidago canadensis. The soil multifunctional index (M) is obtained by performing z-score standardization on conventional soil indexes such as soil pH, cation Exchange Capacity (CEC), total Carbon (TC), total Nitrogen (TN), total Hydrogen (TH), total Sulfur (TS), total Phosphorus (TP), total potassium (TK), organic carbon (SOC), soluble organic carbon (DOC), soluble organic nitrogen (DON), quick-acting phosphorus (SAP), microbial Biomass Carbon (MBC), microbial Biomass Nitrogen (MBN) and Microbial Biomass Phosphorus (MBP) and then calculating according to a formula (1), and the carbon fixation index (RI) is obtained by measuring the Soil Organic Carbon (SOC) and the refractory carbon library (RCP) firstly and then calculating according to a formula (2). The formulas (1) and (2) are as follows:|[0079] Formula (1); |[0080] in the formula (1), M i is the soil multifunctional index of a sample i, N is the total number of soil functional variables, x ij is the actual measured value of the j-th soil functional variable of the sample i, u j is the average value of the j-th soil functional variable in a investigated sample, Standard deviation of the jth soil function variable in the investigated samples.|[0081] Formula (2);|[0082] In the formula (2), RI is carbon fixation index, C RCP is carbon content (g/kg) of a soil refractory carbon library, and C SOC is total organic carbon content (g/kg) of soil. |[0083] The testing process comprises collecting invasion damage soil in the invasion area of Solidago canadensis, naturally air-drying, removing obvious plant root system and broken stone by 2mm nylon sieve, and storing in dark for use. Then, a pot experiment of a homogenous garden is carried out in a nursery communicated with the natural environment. The potting experiment was divided into 3 treatments, no carbon-based material (CK treatment), SCB-HW carbon-based material prepared in step (2) of example 1 (SCB-HW treatment) and SCB-LW carbon-based material prepared in comparative example 1 (SCB-LW treatment), each treatment was repeated 3 times. 3g of the carbon-based materials prepared in example 1 and comparative example 1 were thoroughly mixed with 300g of the previously pretreated solidago canadensis invasion-induced soil, and the mixture was transferred to a plastic flowerpot (upper caliber 10cm, lower caliber 8cm, height 10 cm), water was added to 70% of the maximum water holding capacity of the soil, and 50mL was quantitatively watered every two days. After the experimental flowerpot system is stable for 2 weeks, the culture experiment is started under the condition of natural environment temperature and humidity. After 4 weeks of culture, soil was collected and the index of soil samples per pot was determined and the soil versatility and carbon sequestration index was calculated. Soil pH, CEC, TC, TN, TH, TS, TP, TK, DOC, DON, SAP, MBC, MBN and MBP index were measured by reference to soil physicochemical analysis (ChaInGangGang, china forestry Press). The RCP of the soil is measured by referring to the "method for chemical determination of organic carbon component of soil and progress of carbon index study" (Zhang Fangfang, journal of agricultural environmental science). The experimental results are shown in FIG. 1 and Table 1.|[0084] The results of the effect of adding the carbon-based materials prepared in example 1 and comparative example 1 to soil on the versatility and carbon fixation ability of the damaged soil are shown in table 1.|[0085] TABLE 1 influence of carbon-based materials prepared in example 1 and comparative example 1 on soil versatility index and carbon fixation index due to foreign plant invasion|[0086] |[0087] Note that the tabular data is presented in the form of "mean ± standard deviation".|[0088] As can be seen by comparing the CK group, the SCB-HW group and the SCB-LW group, in terms of restoring the versatility of the soil, the addition of the SCB-HW carbon-based material can significantly restore and promote the versatility of the soil damaged by invasion compared with the treatment group (CK) without the carbon-based material. Compared with SCB-LW, the SCB-HW has better effect in restoring soil multifunctionality, mainly due to the optimized physical and chemical structure, the higher-temperature hydrothermal reaction at 260 ℃ remarkably promotes the development of pores of the material, a developed mesoporous-macroporous hierarchical structure and a high specific surface area are formed (the specific surface area of the carbon-based material formed by the hydrothermal carbonization at 260 ℃ is 17.48m 2/g, and the specific surface area of the carbon-based material formed by the hydrothermal carbonization at 180 ℃ is 3.10m 2/g), so that the adsorption capacity of residual sense substances of invasive plants is greatly enhanced, the biotoxicity of the residual sense substances is reduced, a richer perching space is provided for beneficial microorganisms, and the recovery of the diversity of microbial communities and key metabolic activities (such as nutrient circulating enzymes) is effectively promoted. Meanwhile, the activation degree of mineral components (such as potassium and silicon) in ash at the temperature is higher, so that the effective slow release of nutrients and synergistic passivation of potential pollutants can be realized, and the directional evolution of surface functional groups (such as the formation of stable quinone groups) jointly optimizes the soil microenvironment and more effectively reverses the soil structural damage (the improvement of the stability of aggregates), the biological activity inhibition and the nutrient circulation disorder caused by invasion.|[0089] In terms of improving the carbon fixation capacity of soil, compared with a treatment group without adding the carbon-based material, the addition of the SCB-HW and the SCB-LW carbon-based materials can obviously improve the carbon fixation index of the soil damaged by invasion, but the improvement effect of the SCB-HW carbon-based material (the carbon fixation index of the soil is 0.70) is better than that of the SCB-LW carbon-based material (the carbon fixation index of the soil is 0.61). The SCB-HW is obviously superior to SCB-LW in improving the carbon holding capacity of soil, and has the core that the high-stability and strengthening stabilization effect of a carbon skeleton is that the high-temperature hydrothermal reaction depth of 260 ℃ promotes the aromatic polycondensation reaction of raw materials, a stable sp2 carbon network which has higher polymerization degree and is rich in condensed ring aromatic structures is formed, the biodegradability of the material is obviously enhanced, and the material directly contributes to long-term carbon fixation as a durable carbon warehouse. In addition, the surface chemical characteristics (such as moderate hydrophobicity and stable quinolyl) evolving at the temperature can more efficiently interact with soil organic matters through pi-pi action, hydrogen bonds and possible covalent bonding mechanisms, so that the physical migration and biomineralization loss of active carbon components are effectively reduced, and the chemical protection and stabilization capability of original and newly added organic carbon of the soil is greatly improved.|[0090] Effect example 1 shows that the application effect of the solidago canadensis stalk hydrothermal carbon-based material prepared at 260 ℃ is better than that of the solidago canadensis stalk hydrothermal carbon-based material prepared at 180 ℃.|[0091] Effect example 2|[0092] And (3) measuring and analyzing the improvement performance of the carbon-based materials SCB-HW prepared in the step (2) of the embodiment 1 and the improvement performance of the carbon-based materials SCB-HW4 and SCB-HW12 prepared in the proportion 2 on the multi-functional recovery and carbon retention capacity of the solidago canadensis invasion-induced soil. The soil multi-functional recovery and carbon retention were calculated in the same manner as in effect example 1.|[0093] The test procedure was the same as in effect example 1, and the potting experiment was divided into 4 treatments, namely, no carbon-based material treatment (CK) addition, SCB-HW carbon-based material treatment (SCB-HW) prepared in step (2) of example 1 addition, SCB-HW4 carbon-based material treatment (SCB-HW 4) prepared in comparative example 2 addition, and SCB-HW carbon-based material treatment (SCB-HW 12) prepared in comparative example 2 addition, each treatment being repeated 3 times. The experimental results are shown in Table 2.|[0094] TABLE 2 influence of carbon-based materials prepared in example 1 and comparative example 2 on soil versatility index and carbon fixation index due to foreign plant invasion|[0095] |[0096] Note that the tabular data is presented in the form of "mean ± standard deviation".|[0097] As can be seen from table 2, in terms of restoration of soil versatility, the addition of three carbon-based materials of SCB-HW, SCB-HW4 and SCB-HW12 all improved the versatility of the invading damage-induced soil to a different extent compared to the treatment group (CK) without carbon-based material, wherein the restoration effect of SCB-HW (soil multifunction index of 0.12) was most remarkable, SCB-HW12 times (0.08), and SCB-HW4 was minimally improved (0.04). The method has the advantages that the hydrothermal reaction time is prolonged to 8 hours at 260 ℃, the construction of the optimal pore structure and surface chemical characteristics of the soil function recovery are facilitated, when the hydrothermal time is only 4 hours, carbonization is insufficient, pores are not fully developed, the adsorption and passivation capability of the material to chemical sensing substances are limited, the improvement range of the soil multifunctionality is small, when the hydrothermal time is prolonged to 12 hours, although the aromaticity is further improved, excessive polycondensation is easy to cause partial pore collapse and pore diameter structure singleization, the number of oxygen-containing functional groups on the surface is reduced, the comprehensive regulation capability of the material to chemical sensing substances and nutrients is weakened, and the repair effect is superior to that of SCB-HW4, but is still lower than that of SCB-HW prepared under the condition of 8 hours.|[0098] In terms of improving the carbon fixation capacity of soil, compared with CK treatment, the addition of three carbon-based materials of SCB-HW4, SCB-HW12 and SCB-HW can improve the carbon fixation index of the invaded damaged soil, wherein the carbon fixation index of the SCB-HW is the highest (0.70), the carbon fixation index of the SCB-HW is the next 12 (0.67), and the carbon fixation index of the SCB-HW4 is the lowest (0.62). This shows that a better balance is achieved for the carbon skeleton formed at a hydrothermal reaction time of 8h at 260 ℃. On one hand, the 8h hydrothermal reaction can ensure sufficient aromatization polycondensation, and simultaneously, a proper amount of pore structures and a certain amount of oxygen-containing functional groups are reserved, so that the material has higher biodegradability, and can form a stable complex with soil organic matters in a pi-pi action, hydrogen bonds and other modes, thereby more effectively reducing migration and mineralization of active organic carbon, and on the other hand, a properly developed pore structure is beneficial to the organic carbon to be embedded and embedded, and the physical protection effect is enhanced. In contrast, the SCB-HW4 carbon network prepared under the condition of 4 hours is not perfect, the stable carbon proportion is lower, and the carbon fixation index is improved only to a limited extent, while the SCB-HW12 prepared under the condition of 12 hours has higher aromaticity, but excessive polycondensation and pore degradation weaken the physical-chemical synergistic protection capability on soil organic carbon, so that the carbon fixation index is higher than that of the SCB-HW4 but still not as high as that of the SCB-HW.|[0099] Effect example 2 shows that in the solidago canadensis straw hydro-thermal carbon-based material prepared under the condition of 260 ℃, the SCB-HW with the hydro-thermal reaction time of 8h is superior to the SCB-HW4 and the SCB-HW12 prepared under the conditions of 4h and 12h in terms of improving the versatility and carbon holding capacity of the invasion-induced damage soil, and the preferred hydro-thermal reaction time of 8h has obvious technical effect and is one of key parameters for realizing the best restoration and carbon fixing performance.|[0100] Effect example 3|[0101] The carbon-based materials SCB-HW and SCB-HN prepared in the example 1 were assayed and analyzed for the improvement of the recovery of the versatility and the carbon retention ability of the soil caused by invasion of Solidago canadensis. The soil multi-functional recovery and carbon retention were calculated in the same manner as in effect example 1.|[0102] The test procedure was the same as in effect example 1, except that the potting experiment was divided into 3 treatments, i.e., no carbon-based material treatment (CK) added, SCB-HN carbon-based material treatment (SCB-HN) prepared in example 1 added, and SCB-HW carbon-based material treatment (SCB-HW) prepared in step (2) of example 1 added, each treatment being repeated 3 times. The experimental results are shown in FIG. 1.|[0103] FIG. 1 is a graph showing the effect of adding the SCB-HW carbon-based material and the SCB-HN carbon-based material prepared in example 1 to soil on the versatility and carbon sequestration ability of the soil. As can be seen from fig. 1, in the aspect of restoring the soil versatility, the addition of both SCB-HN and SCB-HW carbon-based materials can significantly restore and enhance the versatility of the invading damage-induced soil, compared to the treatment group without adding the carbon-based material, but the restoration effect of SCB-HN carbon-based material (soil multifunction index of 0.69) is higher than that of SCB-HW carbon-based material (soil multifunction index of 0.12). Compared with SCB-HW, SCB-HN has better effect in restoring soil multifunctionality, and the core is the huge specific surface area and high dispersibility caused by the superfine particle size. The scale of the near nanometer grade endows SCB-HN carbon-based material with extremely high specific surface area and rich surface active sites, so that the SCB-HN carbon-based material can more efficiently and uniformly adsorb and passivate residual solidago canadensis allelopathy substances in soil, and the inhibition effect of the solidago canadensis on indigenous microorganisms and plants is remarkably reduced. Meanwhile, the ultrafine particles can penetrate into soil micropores and rhizosphere micro-domains, provide order-of-magnitude multiplication colonization sites for beneficial microorganisms, greatly promote reconstruction of microbial community diversity and recovery of key enzyme activities (such as dehydrogenase and phosphatase), and accelerate nutrient circulation processes. In addition, the compact network structure formed by the near-nanoscale particles in the soil can bridge soil particles more effectively and promote the formation of stable aggregates, so that the physical structure (ventilation and water retention) and biochemical functions of the soil are systematically improved. The SCB-HW carbon-based material is a millimeter-sized material, and has greatly limited adsorption capacity, microorganism carrier effect and structure improvement efficiency due to overlarge particle size, low specific surface area and poor dispersibility.|[0104] In terms of improving the carbon fixation capacity of soil, compared with a treatment group without adding the carbon-based material, the addition of the SCB-HN and the SCB-HW carbon-based materials can obviously improve the carbon fixation index of the soil damaged by invasion, but the improvement effect of the SCB-HN carbon-based material (the carbon fixation index of the soil is 0.77) is 10 percent higher than that of the SCB-HW carbon-based material (the carbon fixation index of the soil is 0.70). SCB-HN is obviously superior to SCB-HW in improving the carbon holding capacity of soil, and the key mechanism is the physical protection and chemical stabilization of the nano-scale reinforcement. The near-nano particles can be highly dispersed and tightly embedded into a soil matrix due to the extremely small size and the huge specific surface area, are particularly easy to enter the inside of an aggregate or combine with the surface of minerals to form a physical barrier, effectively wrap and protect active organic carbon components, reduce the contact of the active organic carbon components with microorganisms and enzymes, and reduce the mineralization rate. More importantly, the superfine particle size enables the superfine particle size to expose exponentially growing surface functional groups (such as carboxyl, phenolic hydroxyl and quinone groups), and the groups can be tightly combined with soil organic matter molecules through strong chemical adsorption (such as coordination bonds, hydrogen bonds and pi-pi actions) to form a stable organic-mineral-carbon complex, so that chemical bonding stabilization on original and newly added organic carbon of the soil is remarkably enhanced. The SCB-HW has small specific surface area, low surface activity and difficult effective dispersion to a soil micro-domain, has weak physical isolation effect, and has severely insufficient chemical bonding capability with soil organic matters, so that the SCB-HW has limited contribution to long-term stabilization of a carbon reservoir.|[0105] Effect example 3 shows that the application effect of the near-nanoscale solidago canadensis straw hydro-carbon-based material is better than that of the non-near-nanoscale solidago canadensis straw hydro-carbon-based material.|[0106] Effect example 4|[0107] The carbon-based materials SCB-HN and SCB-HN2 and SCB-HN12 prepared in the example 1 and the comparative example 3 are determined and analyzed to restore the multi-functionality of the soil and improve the carbon holding capacity caused by the invasion of solidago canadensis. The soil multi-functional recovery and carbon retention were calculated in the same manner as in effect example 1.|[0108] The test procedure was the same as in effect example 1, except that the potting experiment was divided into 4 treatments, namely, no carbon-based material treatment (CK), SCB-HN carbon-based material treatment (SCB-HN) prepared in example 1, SCB-HN2 carbon-based material treatment (SCB-HN 2) prepared in comparative example 3 and SCB-HN12 carbon-based material treatment (SCB-HN 12) prepared in comparative example 3, each treatment being repeated 3 times. The experimental results are shown in Table 3.|[0109] TABLE 3 influence of carbon-based materials prepared in example 1 and comparative example 3 on soil versatility index and carbon fixation index due to foreign plant invasion|[0110] |[0111] Note that the tabular data is presented in the form of "mean ± standard deviation".|[0112] As can be seen from table 3, there is a significant difference in the effect of the addition of three near-nanocarbon-based materials SCB-HN, SCB-HN2 and SCB-HN12 on the improvement of the versatility of the intrusion-induced soil, compared to the treatment group without the addition of the carbon-based material, in terms of restoration of the versatility of the soil. Among them, the recovery effect of SCB-HN treatment prepared by ball milling for 6 hours (soil versatility index of 0.69) is most remarkable, SCB-HN12 treatment is performed for a second time (0.62), while SCB-HN2 treatment prepared by ball milling for 2 hours cannot improve soil versatility, but rather exhibits negative shift (-0.59). This shows that ball milling time is one of the key parameters for regulating and controlling the functional effect of near-nano carbon based materials under the same raw materials and hydrothermal conditions. When the ball milling time is only 2 hours, the grain diameter refinement degree is limited, the increase of the specific surface area and the surface active site is not obvious, the material still keeps more coarse grain structures, the rhizosphere and the aggregate micro-domain are difficult to fully enter, the adsorption and passivation capability of chemical sensing substances are limited, and the functional microorganisms are difficult to provide enough colonization sites, even certain disturbance is generated to the soil micro-environment due to the problems of unstable grain diameter distribution, local aggregation and the like, so that the multifunction is not effectively recovered. In contrast, when the ball milling time is prolonged to 6 hours, the particle size of the material is reduced to be near nano-scale, the specific surface area and the exposure degree of the surface functional groups are obviously improved, particles can be more uniformly dispersed in soil micropores and rhizosphere areas, and efficiently adsorb and slowly release sensing substances, a large amount of microorganism adhesion and growth spaces are provided, and the comprehensive recovery of the physical and chemical properties, the microorganism diversity and the key enzyme activity of the soil is cooperatively promoted, so that the optimal effect is shown in the aspect of improving the multifunctionality. Further prolonging the ball milling time to 12h, while still keeping a higher multi-functional index (0.62), the repairing effect is lower than that of SCB-HN but better than that of SCB-HN2 because the long-time strong mechanical force is easy to cause collapse of partial pore structures, too fine particles to agglomerate and mechanical damage of surface functional groups, so that the material is slightly inferior to 6h treatment in the aspects of expanding microorganism habitat space and optimizing pore connectivity.|[0113] In terms of improving the carbon fixation capacity of soil, compared with CK treatment (the carbon fixation index of the soil is 0.52), the addition of three near-nano carbon-based materials of SCB-HN2, SCB-HN12 and SCB-HN can improve the carbon fixation index of the soil caused by invasion, wherein the improving effect of the SCB-HN is most prominent (the carbon fixation index of the soil is 0.77) and is remarkably higher than that of the SCB-HN12 (0.74) and the SCB-HN2 (0.68). This demonstrates that carbon stability can be optimized by combining 6h ball milling treatment on the basis of 260 ℃ hydrothermal carbonization. On one hand, moderate ball milling time is beneficial to breaking large particles and exposing more mesoporous-microporous structures and oxygen-containing functional groups, so that the carbon-based material can stabilize soil organic carbon in an aggregate or on the surface of minerals through a double way of physical embedding and chemical bonding (pi-pi action, hydrogen bonding and the like), and the synergistic effect of physical protection and chemical protection is enhanced, and on the other hand, the 6-hour ball milling can not excessively destroy an aromatic carbon network and key functional groups, so that the material self maintains higher biodegradability and the binding capability with soil organic matters. In contrast, SCB-HN2 prepared by 2h ball milling has limited effective surface sites capable of participating in physical-chemical stabilization of organic carbon due to insufficient grain size refinement and insufficient development of pore structure, and SCB-HN12 prepared by 12h ball milling has smaller lifting amplitude of carbon fixation index, while partial micropores-mesopores are compacted or collapsed due to long-time mechanical action although the grain size is finer, and surface functional groups are subjected to a certain degree of shearing damage, so that the surface functional groups are slightly inferior to SCB-HN in long-term carbon stabilization.|[0114] Effect example 4 shows that under the same raw materials and hydrothermal conditions, the near nanoscale Solidago canadensis straw carbon-based material SCB-HN prepared by ball milling time of 6h is superior to SCB-HN2 and SCB-HN12 prepared under the ball milling conditions of 2h and 12h in terms of improving the multifunctionality and carbon holding capacity of the invasion-induced soil, and the preferential 6h ball milling modification time of the invention has remarkable technical effects and is one of key parameters for realizing optimal restoration and carbon fixing performance of the carbon-based material.|[0115] Effect example 5|[0116] The carbon-based materials SCB-HN, CB-HN and PB-HN prepared in the examples 1, 4 and 5 were analyzed for the improvement of the multi-functional recovery and carbon retention ability of the solidago canadensis invasion-induced soil. The soil multi-functional recovery and carbon retention were calculated in the same manner as in effect example 1.|[0117] The test procedure was the same as in effect example 1, except that the potting experiment was divided into 4 treatments, namely, no carbon-based material treatment (CK), SCB-HN carbon-based material treatment (SCB-HN) prepared in example 1, CB-HN carbon-based material treatment (CB-HN) prepared in comparative example 4 and PB-HN carbon-based material treatment (PB-HN) prepared in comparative example 5, each treatment being repeated 3 times. The experimental results are shown in FIG. 2.|[0118] FIG. 2 is a graph showing the effect of adding the SCB-HN carbon-based material prepared in example 1, the CB-HN carbon-based material prepared in comparative example 4, and the PB-HN carbon-based material prepared in comparative example 5 to soil, on the versatility and carbon fixing ability of the soil. As can be seen from fig. 2, in the aspect of restoring the soil versatility, the addition of SCB-HN and CB-HN carbon-based materials can significantly restore and enhance the versatility of the invasion-induced soil, compared to the treatment group without carbon-based materials, wherein the effect of SCB-HN is most prominent (soil versatility index of 0.69) and significantly higher than CB-HN (soil versatility index of 0.14) and PB-HN (soil versatility index of-0.28). SCB-HN (Solidago canadensis straw carbon-based material) has better effect in restoring soil versatility compared with CB-HN (corn straw carbon-based material) and PB-HN (peach branch carbon-based material), and is characterized in that the special ash composition and pore structure of the raw materials. The solidago canadensis straw is rich in silicon, potassium and trace metal elements, forms high-activity amorphous silicate and mineral phases in ash of derived carbon, can efficiently adsorb and passivate residual homologous sense substances in soil, lightens the inhibition of the homologous sense substances to microbial communities, and meanwhile, the fiber structure of the raw material forms a developed mesopore-micropore hierarchical system after carbonization, so that the retention capacity of moisture and nutrients and microbial habitat space are remarkably improved, and the stability and biological activity recovery of aggregates of damaged soil are pertinently promoted. The corn straw carbon-based material is low in ash content and insufficient in pore uniformity, and peach branch carbon-based material is dominant in macropores and limited in specific surface area due to lignin derivative, so that the equivalent removal of chemical substances and the synergistic restoration of micro ecology are difficult to realize.|[0119] In terms of improving the carbon fixation capacity of the soil, compared with a treatment group without adding the carbon-based material, the addition of the SCB-HN, CB-HN and PB-HN carbon-based materials can improve the carbon fixation index of the invaded damaged soil, wherein the effect of the SCB-HN is most prominent (the carbon fixation index of the soil is 0.77) and is obviously higher than that of the CB-HN (the carbon fixation index of the soil is 0.67) and the PB-HN (the carbon fixation index of the soil is 0.56). The advantage of SCB-HN in carbon holding capacity is derived from a double stabilization mechanism given by raw materials, namely the high silicon characteristic of the solidago canadensis straw promotes the formation of a silicon-carbon composite skeleton in carbon, a siliceous coating layer effectively insulates microbial attack and greatly improves the stability of the carbon, and meanwhile, the specific proportion of lignin/cellulose in the raw materials is carbonized to generate a high proportion fused ring aromatic structure and surface quinolyl groups, so that soil organic matters can be strongly fixed through chemical bonding (such as Si-O-C covalent bonds and quinone-phenol redox couples) to form an anti-degradation organic-mineral complex. In contrast, the low-carbonization aromatic structure of the corn straw carbon-based material CB-HN is easy to mineralize, the peach branch carbon-based material PB-HN has strong hydrophobicity but sparse bonding sites, and the contribution of the low-carbonization aromatic structure to the long-term stability of the soil carbon reservoir is obviously weaker than that of the SCB-HN.|[0120] Effect example 5 shows that under the same preparation conditions, the application effect of the carbon-based material prepared by taking solidago canadensis as a raw material is better than that of the carbon-based material prepared by taking corn stalks and peach branches as raw materials.|[0121] The experimental results of comprehensive effect examples 1-5 show that the carbon-based material (SCB-HN) prepared by taking solidago canadensis as a raw material and modifying the solidago canadensis through combining the hydrothermal carbonization at 260 ℃ and the near-nanoscale grinding for 6 hours has the best effect of restoring the multifunctionality of the soil and improving the carbon holding capacity caused by the invasion of solidago canadensis.|[0122] The present invention is not limited to the above-mentioned embodiments, and any changes or substitutions that can be easily understood by those skilled in the art within the technical scope of the present invention are intended to be included in the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope of the claims. (CN121426099)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of soil remediation and carbon fixation and sink enhancement, and particularly relates to a near-nano carbon-based material for restoring functions and improving carbon fixation capacity of soil caused by invasion of foreign plants and a preparation method thereof.|BACKGROUND ART|[0002] Canadian Solidago (Solidago canadensis) is introduced into China since the 30 s of the 20 th century as a typical exotic invasive plant, and has spread to the east, south, middle and west areas of China, causing significant harm to farmlands and natural ecosystems. The species has strong competitiveness and is easy to form a single optimal community, so that the original local vegetation diversity is obviously reduced, the community structure is simplified and the underground biomass distribution is changed. The change of the vegetation community structure not only directly affects the composition of root secretions and the carbon flow input mode, but also indirectly drives the reconstruction of the soil microbial community by changing the rhizosphere environment. A large number of researches show that the solidago canadensis has obvious chemosensory effect in the invasion process, can continuously release phenolic acid, terpenoid and other chemosensory substances, and can inhibit the activity of key soil functional microorganisms (such as ammonia oxidizing bacteria, phosphate solubilizing bacteria, cellulose decomposing bacteria, arbuscular mycorrhizal fungi and the like), so that the diversity of the microorganisms is reduced, the community structure is abnormal and the nitrogen and phosphorus circulation function is weakened. Meanwhile, due to single vegetation community, reduced underground carbon source input and reduced quality after invasion, the bacterial/fungal proportion of soil shifts, so that lignin degradation flora is inhibited, and the formation of soil aggregates and the construction of a stable carbon reservoir (such as mineral bound organic carbon) are further affected. Thus, the invasion of solidago canadensis shows a chained effect of vegetation community change-rhizosphere environment change-microbial community change-ecological function degradation, and the superimposed toxin-sensing effect finally causes the soil structural damage, the acceleration of mineralization of organic matters and the degradation of carbon fixation capacity. In addition, even if the invasion of solidago canadensis is treated by methods such as manual pulling, cutting, burning, chemical prevention and control, the residual allelopathy substances cannot be eliminated, and the ecological functions of soil caused by vegetation degradation and microorganism imbalance cannot be recovered|[0003] Therefore, an effective treatment and restoration means for the damage soil caused by invasion of the exotic plant solidago canadensis is not available at present. The charcoal-based materials such as biochar have certain adsorption and soil physicochemical property improving effects, and are regarded as potential repairing materials. However, the conventional carbon-based materials prepared by pyrolysis still have various limitations, such as large particles, limited specific surface area, insufficient dispersibility and limited surface functional groups, are difficult to penetrate into rhizosphere or aggregate micro-domain environments, lack the capability of specific action with chemosensory toxins, and are difficult to realize targeted restoration and carbon library stabilization enhancement of soil degradation caused by invasion of solidago canadensis.|DISCLOSURE|Disclosure of Invention|[0004] In order to solve the technical problems, the invention provides a near-nano carbon-based material for restoring the soil functions and improving the carbon-fixing capability caused by foreign plant invasion and a preparation method thereof. Aiming at the problems of the loss of the function and the reduction of the carbon sink capacity of the invaded soil caused by the invasion of solidago canadensis, the near-nano carbon-based material prepared by the invention can effectively promote the reconstruction of the soil structure, the functional recovery and the enhancement of the formation capacity of a stable carbon reservoir, thereby simultaneously improving the soil multifunctionality and the carbon holding capacity. Meanwhile, the method takes the solidago canadensis straw as the main raw material, realizes an ecological closed-loop path for intrusion treatment by using the waste biomass of the invasive plant through recycling, and has the advantages of easily available raw materials, environmental friendliness, controllable cost, large-scale application and the like.|[0005] In order to achieve the above purpose, the present invention provides the following technical solutions:|[0006] the invention provides a preparation method of a near-nano carbon-based material for restoring functions and improving carbon-fixing capacity of soil caused by invasion of foreign plants, wherein the foreign plants are solidago canadensis, and the preparation method comprises the following steps: |[0007] (1) Crushing and sieving Canadian one-branch yellow flower stalks to obtain Canadian one-branch yellow flower stalk granules; |[0008] (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water, and performing hydrothermal reaction to obtain a Canadian herba Solidaginis stalk hydrothermal carbonization product; |[0009] (3) Ball milling is carried out on the solidago canadensis stalk hydrothermal carbonization product obtained in the step (2), and then sieving is carried out, so as to obtain the near-nano carbon-based material. |[0010] The invention is based on the ecological closed-loop concept of 'treating invasive damage with invasive organisms', and utilizes the characteristic that the solidago canadensis straw is rich in structural silicon and lignin derived aromatic carbon to directionally convert the solidago canadensis straw into near-nano carbon-based material, the silicon component can effectively deactivate homologous influenza toxin, and the high-aromaticity carbon skeleton cooperates with the nano structure to reconstruct soil aggregate, activate microorganism function and strengthen organic carbon-mineral bonding, thereby accurately reversing the degradation of the invasive induced soil function.|[0011] Further, in the step (1), the particle size of the Canadian one-branch yellow flower stalk particles is 180-250 μm.|[0012] Further, in the step (1), the mass ratio of the Canadian paris polyphylla stalk particles to the deionized water is 1:10.|[0013] Further, in the step (2), the hydrothermal reaction is performed under autogenous pressure, the temperature of the hydrothermal reaction is 260 ℃, and the time of the hydrothermal reaction is 8 hours. Further, in the step (2), the steps of filtering, washing and drying are further included after the hydrothermal reaction is finished.|[0014] Further, the washing process is to alternately wash with deionized water and absolute ethyl alcohol and then wash with sodium hydroxide solution with concentration of 0.1mol/L for 2-3 times.|[0015] Further, in the step (3), the ball material mass ratio of the ball milling is 10:1, the ball milling speed is 500rpm, the ball milling time is 30min after 2-12h of ball milling, and the ball milling-rest process is repeated for 3 times.|[0016] Further, in the step (3), the ball milling equipment is a planetary ball mill, and the ball stone used for ball milling is stainless steel ball stone with the diameter of 10 mm.|[0017] Further, in the step (3), the mesh number of the screen mesh used for the sieving is 4000 mesh.|[0018] The invention also provides the near-nano carbon-based material which is prepared by the preparation method and has the advantages of restoring the function of the soil caused by invasion of the foreign plant and improving the carbon-fixing capability.|[0019] The invention also provides application of the near-nano carbon-based material for improving the function recovery and carbon fixation capacity of the foreign plant invasion-induced damage soil in improving the function recovery and carbon fixation capacity of the foreign plant invasion-induced damage soil.|[0020] Compared with the prior art, the invention has the following advantages and technical effects:|[0021] (1) The near-nano carbon-based material prepared by the invention can realize the multifunctional recovery of the solidifiable soil caused by solidago canadensis and the improvement of the carbon fixation capacity. |[0022] (2) The invention optimizes the physical and chemical structure of the near-nano carbon-based material by controlling the temperature of the hydrothermal reaction, lays a foundation for in-situ restoration and carbon fixation synergy of soil, can remarkably improve the versatility of the soil, has the core mechanism that a developed mesoporous-macroporous hierarchical structure and a high specific surface area are formed by 260 ℃ hydrothermal carbonization (the specific surface area of the carbon-based material formed by 260 ℃ hydrothermal carbonization is 17.48m < 2 >/g, and the specific surface area of the carbon-based material formed by 180 ℃ hydrothermal carbonization is 3.10m < 2 >/g), enhances the adsorption capacity of the carbon-based material on the residual sensing substances of Solidago canadensis, effectively reduces the biotoxicity, and passivates pollutants in cooperation with mineral components such as silicon, potassium and the like in activated ash, promotes the diversity recovery of microbial communities, and systematically reverses the structural damage and the nutrient circulation disorder of the soil. The invention also improves the carbon fixation index of the near-nano carbon-based material by controlling the temperature of the hydrothermal reaction, which is derived from a stable carbon network formed by 260 ℃ hydrothermal carbonization deep aromatization polycondensation reaction, improves the self biodegradation resistance of the carbon-based material, and reduces migration and mineralization loss of active carbon components by pi-pi action or hydrogen bonding between the surface stable quinone groups and soil organic matters, thereby realizing long-acting carbon fixation.|[0023] (3) The soil multifunction value of the near-nano carbon-based material prepared by the invention is 475 percent higher than that of the carbon-based material (comparative example 2) prepared without ball milling modification treatment, and the near-nano carbon-based material has the advantages of huge specific surface area and high dispersibility caused by ultrafine particle size (near-nano grade), and the characteristics enable carbon particles to efficiently adsorb and passivate allelochemicals, penetrate into soil micropores and rhizosphere areas, provide exponentially growing microbial colonization sites, and meanwhile, compact network formed by particles bridge soil particles, enhance the stability of agglomerates, systematically improve physical structures such as ventilation, water holding and the like, and pertinently repair microecological imbalance caused by invasion. The carbon fixation index of the near-nano carbon-based material prepared by the method is 10% higher than that of the carbon-based material prepared without ball milling modification treatment, and the key mechanism is that nano-scale physical isolation and chemical bonding are double-action, ultrafine particles are embedded into the soil matrix (such as an aggregate or a mineral surface) to form a physical barrier to reduce the contact of organic carbon and microorganisms, and a large number of surface functional groups (such as carboxyl and phenolic hydroxyl) are exposed to be combined with organic matters strongly through coordination bonds or pi-pi action to form a stable organic-mineral-carbon complex, so that the long-term stability of a carbon warehouse is remarkably improved. Therefore, the near-nanoscale ball milling modification treatment serves as a core innovation point of the invention, and the repair precision and the carbon fixing efficiency of the carbon-based material are substantially enhanced through the size effect.|[0024] (4) The soil versatility of the near-nano carbon-based material prepared by utilizing the solidago canadensis is obviously higher than that of the near-nano carbon-based material prepared by utilizing corn stalks and peach branches, which is derived from the special ash composition (high potassium content) and pore structure of the raw materials, the amorphous silicate in the ash can effectively passivate homologous substances, and meanwhile, the developed mesopore-micropore system of the near-nano carbon-based material optimizes the water nutrient retention capacity, synergistically promotes the reconstruction of microbial activity, and realizes the targeted restoration of the invasive damaged soil. The carbon fixation index of the near-nano carbon-based material prepared by utilizing solidago canadensis is superior to that of the near-nano carbon-based material prepared by utilizing corn stalks and peach branches, and the core mechanism is a silicon-carbon composite skeleton with high silicon characteristics of raw materials and a surface quinone base derived from specific lignin proportion. The near-nano carbon-based material prepared by the method is used for fixing organic matters through chemical bonding (such as Si-O-C covalent bonding), so that a degradation-resistant complex is formed, and other raw materials (low aromaticity of corn straw carbon and sparse bonding sites of peach branch carbon) cannot provide equal-length stabilization protection. Therefore, the invasive species Solidago canadensis is taken as the raw material, so that the problem of difficult treatment of the Solidago canadensis biomass waste can be solved, the waste is used for recycling, and the pertinence of in-situ repair and the sustainability of carbon sequestration can be enhanced.|[0025] In conclusion, the method and the device cooperatively improve the in-situ restoration capacity and the carbon fixation and exchange enhancement capacity of the solidago canadensis induced damage farmland soil through triple optimization of the hydrothermal carbonization temperature (260 ℃), the particle size (near nano-scale) and the raw material (solidago canadensis), and provide an efficient and environment-friendly technical path for the invasion soil treatment.|DRAWINGS DESCRIPTION|[0026] The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention. In the drawings:|[0027] FIG. 1 is a graph showing the effect of adding the SCB-HN carbon-based material and the SCB-HW carbon-based material prepared in example 1 to soil on the versatility and carbon sequestration ability of the soil; |[0028] FIG. 2 is a graph showing the effect of adding the SCB-HN carbon-based material prepared in example 1, the CB-HN carbon-based material prepared in comparative example 4, and the PB-HN carbon-based material prepared in comparative example 5 to soil, on the versatility and carbon fixing ability of the soil. |INVENTION MODE|Detailed Description|[0029] The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.|[0030] In order that the above-recited objects, features and advantages of the present invention will become more readily apparent, a more particular description of the invention will be rendered by reference to the appended drawings and appended detailed description.|[0031] The embodiment of the invention provides a preparation method of a near-nano carbon-based material with enhanced carbon-solid capacity and recovery of soil functions caused by invasion of solidago canadensis serving as an external plant, wherein the external plant is solidago canadensis, and the preparation method comprises the following steps:|[0032] (1) Crushing and sieving Canadian one-branch yellow flower stalks to obtain Canadian one-branch yellow flower stalk granules; |[0033] (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water, and performing hydrothermal reaction to obtain a Canadian herba Solidaginis stalk hydrothermal carbonization product; |[0034] (3) Ball milling is carried out on the solidago canadensis stalk hydrothermal carbonization product obtained in the step (2), and then sieving is carried out, so as to obtain the near-nano carbon-based material. |[0035] In a preferred embodiment, in the step (1), the step of washing and drying is further included before the crushing, and the drying temperature is 60 ℃. According to the invention, impurities such as soil on the surface of the solidago canadensis stalks are removed by cleaning.|[0036] In a preferred embodiment, in step (1), the sieving is a 60 mesh sieve.|[0037] In a preferred embodiment, in step (1), the particle size of the Canadian one-branch yellow flower stalk particles is 180-250 μm.|[0038] In a preferred embodiment, in the step (2), the mass ratio of the Canadian paris polyphylla stalk particles to deionized water is 1:10.|[0039] In a preferred embodiment, in step (2), the hydrothermal reaction is carried out under autogenous pressure, the temperature of the hydrothermal reaction is 260 ℃, and the time of the hydrothermal reaction is 8 hours.|[0040] In a preferred embodiment, in step (2), the hydrothermal reaction further comprises the steps of filtering, washing and drying after the completion of the hydrothermal reaction.|[0041] In a preferred embodiment, the washing is performed by first alternately washing with deionized water and absolute ethanol, and then washing 2-3 times with sodium hydroxide solution having a concentration of 0.1 mol/L. The purpose of the invention is to remove acid and phenol soluble impurities, activate oxygen-containing functional groups on the surface of the carbon, improve the purity, dispersibility and specific surface area of the material, and enhance the adsorption, chemical substance passivation and mineral binding capacity of the material, thereby remarkably improving the repairing and carbon fixing effects.|[0042] In a preferred embodiment, in the step (3), the ball mass ratio of the ball milling is 10:1, the ball milling speed is 500rpm, the ball milling time is 2-12h, and then the ball milling is stopped for 30min, the ball milling-stopping process is repeated for 3 times, and more preferably the ball milling time is 6h.|[0043] In a preferred embodiment, in the step (3), the ball milling equipment is a planetary ball mill, and the ball stone used for ball milling is stainless steel ball stone with the diameter of 10 mm.|[0044] In a preferred embodiment, in step (3), the mesh size of the screen used for the sieving is 4000 mesh.|[0045] The invention provides a near-nano carbon-based material which is prepared by the preparation method and is prepared from exotic plants, namely solidifiable by carbon and is improved in the function recovery and carbon fixation capacity of damaged soil caused by invasion of solidago canadensis.|[0046] The invention also provides application of the near-nano carbon-based material for improving the function recovery and carbon fixation capacity of the exotic plant solidago canadensis invasion-induced damage soil in improving the function recovery and carbon fixation capacity of the exotic plant invasion-induced damage soil.|[0047] In the examples of the present invention, room temperature refers to "25.+ -. 2 ℃.|[0048] Unless otherwise specified, the starting materials in the examples of the present invention were all obtained by commercial purchase.|[0049] Example 1|[0050] A preparation method of a near-nano carbon-based material for restoring functions and improving carbon-fixing capacity of soil caused by invasion of foreign plants comprises the following specific steps:|[0051] (1) Collecting Canadian herba Solidaginis stalks, cleaning surface impurities, drying at 60 ℃, pulverizing, sieving with 60 mesh sieve, and collecting Canadian herba Solidaginis stalk particles with particle size of 180-250 μm; |[0052] (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring the mixture into a hydrothermal reaction kettle, heating the mixture to 260 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 260 ℃ and autogenous pressure, cooling the mixture to room temperature, and filtering the mixture to obtain a solid residue; |[0053] (3) Transferring the canadian solidago stalk hydrothermal carbonized product obtained in the step (2) into a planetary ball mill, wherein the ball stones in the planetary ball mill are stainless steel ball stones with the diameter of 10mm, the ball material mass ratio is 10:1, the ball milling speed is 500rpm, the ball milling is carried out for 6 hours, the ball milling is carried out for 30 minutes, the ball milling-rest process is repeated for 3 times, and then the materials pass through a 4000-mesh sieve to obtain the near-nanoscale canadian solidago stalk carbon-based material which is marked as SCB-HN. |[0054] Comparative example 1|[0055] The difference from example 1 is that the temperature of the hydrothermal reaction is 180 ℃ and the ball milling modification treatment is not carried out, and the specific steps are as follows:|[0056] (1) Collecting Canadian herba Solidaginis stalks, cleaning surface impurities, drying at 60 ℃, pulverizing, sieving with 60 mesh sieve, and collecting Canadian herba Solidaginis stalk particles with particle size of 180-250 μm; |[0057] (2) Mixing Canadian herba Solani Lyrati stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring into a hydrothermal reaction kettle, heating to 180 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 180 ℃ and autogenous pressure, cooling to room temperature, filtering to obtain a solid residue, alternately cleaning the obtained solid residue with deionized water and absolute ethyl alcohol, then washing for 2 times with a sodium hydroxide solution with a concentration of 0.1mol/L, vacuum drying, and sieving with a 500-mesh sieve to obtain a Canadian herba Solani Lyrati stalk hydrothermal carbonization product, which is marked as SCB-LW. |[0058] Comparative example 2|[0059] The only difference from example 1 is that the time of hydrothermal reaction was changed without ball milling modification treatment, and the specific steps were as follows:|[0060] (1) Collecting Canadian herba Solidaginis stalks, cleaning surface impurities, drying at 60 ℃, pulverizing, sieving with 60 mesh sieve, and collecting Canadian herba Solidaginis stalk particles with particle size of 180-250 μm; |[0061] (2) Mixing the Canadian herba Solidaginis stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring into a hydrothermal reaction kettle, heating to 260 ℃, respectively carrying out hydrothermal reaction for 4h and 12h under the conditions of 260 ℃ and autogenous pressure, cooling to room temperature, filtering to obtain a solid residue, alternately cleaning the obtained solid residue with deionized water and absolute ethyl alcohol, then washing for 2 times with a sodium hydroxide solution with a concentration of 0.1mol/L, and carrying out vacuum drying to obtain Canadian herba Solidaginis stalk hydrothermal carbonization products which are respectively marked as SCB-HW4 and SCB-HW12. |[0062] Comparative example 3|[0063] The difference from example 1 is that the ball milling modification treatment time is respectively 2h and 12h, and the specific steps are as follows:|[0064] (1) Collecting Canadian herba Solidaginis stalks, cleaning surface impurities, drying at 60 ℃, pulverizing, sieving with 60 mesh sieve, and collecting Canadian herba Solidaginis stalk particles with particle size of 180-250 μm; |[0065] (2) Mixing the Canadian herba Solani first-branch yellow stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring the mixture into a hydrothermal reaction kettle, heating the mixture to 260 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 260 ℃ and autogenous pressure, cooling the mixture to room temperature, and filtering the mixture to obtain a solid residue; |[0066] (3) Transferring the Canadian goldenrod stalk hydrothermal carbonization product obtained in the step (2) into a planetary ball mill, wherein the ball stones in the planetary ball mill are stainless steel ball stones with the diameter of 10mm, the ball material mass ratio is 10:1, the ball milling speed is 500rpm, the ball milling is respectively carried out for 2 hours and 12 hours, then the ball milling is carried out for rest for 30 minutes, the ball milling-rest process is repeated for 3 times, and then the materials pass through a 4000-mesh sieve to obtain near-nanoscale Canadian goldenrod stalk carbon-based materials which are respectively marked as SCB-HN2 and SCB-HN12. |[0067] Comparative example 4|[0068] The difference with example 1 is that the solidago canadensis straw is replaced by corn straw to prepare the near-nanoscale corn straw carbon-based material, which comprises the following specific steps:|[0069] (1) Collecting corn straw, cleaning surface impurities, drying at 60 ℃, crushing, sieving with a 60-mesh sieve, and collecting corn straw particles with the particle size of 180-250 mu m; |[0070] (2) Mixing the corn stalk particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring the mixture into a hydrothermal reaction kettle, heating the mixture to 260 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 260 ℃ and autogenous pressure, cooling the mixture to room temperature, and filtering the mixture to obtain a solid residue; |[0071] (3) Transferring the corn stalk hydrothermal carbonized product obtained in the step (2) into a planetary ball mill, wherein the ball stones in the planetary ball mill are stainless steel ball stones with the diameter of 10mm, the ball material mass ratio is 10:1, the ball milling speed is 500rpm, the ball milling is carried out for 6 hours, the rest is carried out for 30 minutes, the ball milling-rest process is repeated for 3 times, and then the corn stalk carbon-based material with the near nano-grade is obtained through a 4000-mesh sieve and is recorded as CB-HN. |[0072] Comparative example 5|[0073] The difference with example 1 is that the solidago canadensis straw is replaced by peach branches, and the preparation method of the near-nanoscale peach branch carbon-based material comprises the following specific steps:|[0074] (1) Collecting peach branches, cleaning surface impurities, drying at 60 ℃, crushing, sieving with a 60-mesh sieve, and collecting peach branch particles with the particle size of 180-250 mu m; |[0075] (2) Mixing the peach branch particles obtained in the step (1) with deionized water according to a mass ratio of 1:10, transferring the mixture into a hydrothermal reaction kettle, heating the mixture to 260 ℃, carrying out hydrothermal reaction for 8 hours under the conditions of 260 ℃ and autogenous pressure, cooling the mixture to room temperature, and filtering the mixture to obtain a solid residue; |[0076] (3) Transferring the peach tree branch hydrothermal carbonization product obtained in the step (2) into a planetary ball mill, wherein the ball stones in the planetary ball mill are stainless steel ball stones with the diameter of 10mm, the ball material mass ratio is 10:1, the ball milling speed is 500rpm, the ball milling is carried out for 6 hours, the rest is carried out for 30 minutes, the ball milling-rest process is repeated for 3 times, and then the peach tree branch charcoal base material with near nano-scale is obtained through a 4000-mesh sieve and is recorded as PB-HN. |[0077] Effect example 1|[0078] The carbon-based material (SCB-HW) prepared in the step (2) of the example 1 and the carbon-based material (SCB-LW) prepared in the comparative example 1 were analyzed for the improvement of the multi-functional recovery and carbon retention ability of the soil caused by the invasion of solidago canadensis. The soil multifunctional index (M) is obtained by performing z-score standardization on conventional soil indexes such as soil pH, cation Exchange Capacity (CEC), total Carbon (TC), total Nitrogen (TN), total Hydrogen (TH), total Sulfur (TS), total Phosphorus (TP), total potassium (TK), organic carbon (SOC), soluble organic carbon (DOC), soluble organic nitrogen (DON), quick-acting phosphorus (SAP), microbial Biomass Carbon (MBC), microbial Biomass Nitrogen (MBN) and Microbial Biomass Phosphorus (MBP) and then calculating according to a formula (1), and the carbon fixation index (RI) is obtained by measuring the Soil Organic Carbon (SOC) and the refractory carbon library (RCP) firstly and then calculating according to a formula (2). The formulas (1) and (2) are as follows:|[0079] Formula (1); |[0080] in the formula (1), M i is the soil multifunctional index of a sample i, N is the total number of soil functional variables, x ij is the actual measured value of the j-th soil functional variable of the sample i, u j is the average value of the j-th soil functional variable in a investigated sample, Standard deviation of the jth soil function variable in the investigated samples.|[0081] Formula (2);|[0082] In the formula (2), RI is carbon fixation index, C RCP is carbon content (g/kg) of a soil refractory carbon library, and C SOC is total organic carbon content (g/kg) of soil. |[0083] The testing process comprises collecting invasion damage soil in the invasion area of Solidago canadensis, naturally air-drying, removing obvious plant root system and broken stone by 2mm nylon sieve, and storing in dark for use. Then, a pot experiment of a homogenous garden is carried out in a nursery communicated with the natural environment. The potting experiment was divided into 3 treatments, no carbon-based material (CK treatment), SCB-HW carbon-based material prepared in step (2) of example 1 (SCB-HW treatment) and SCB-LW carbon-based material prepared in comparative example 1 (SCB-LW treatment), each treatment was repeated 3 times. 3g of the carbon-based materials prepared in example 1 and comparative example 1 were thoroughly mixed with 300g of the previously pretreated solidago canadensis invasion-induced soil, and the mixture was transferred to a plastic flowerpot (upper caliber 10cm, lower caliber 8cm, height 10 cm), water was added to 70% of the maximum water holding capacity of the soil, and 50mL was quantitatively watered every two days. After the experimental flowerpot system is stable for 2 weeks, the culture experiment is started under the condition of natural environment temperature and humidity. After 4 weeks of culture, soil was collected and the index of soil samples per pot was determined and the soil versatility and carbon sequestration index was calculated. Soil pH, CEC, TC, TN, TH, TS, TP, TK, DOC, DON, SAP, MBC, MBN and MBP index were measured by reference to soil physicochemical analysis (ChaInGangGang, china forestry Press). The RCP of the soil is measured by referring to the "method for chemical determination of organic carbon component of soil and progress of carbon index study" (Zhang Fangfang, journal of agricultural environmental science). The experimental results are shown in FIG. 1 and Table 1.|[0084] The results of the effect of adding the carbon-based materials prepared in example 1 and comparative example 1 to soil on the versatility and carbon fixation ability of the damaged soil are shown in table 1.|[0085] TABLE 1 influence of carbon-based materials prepared in example 1 and comparative example 1 on soil versatility index and carbon fixation index due to foreign plant invasion|[0086] |[0087] Note that the tabular data is presented in the form of "mean ± standard deviation".|[0088] As can be seen by comparing the CK group, the SCB-HW group and the SCB-LW group, in terms of restoring the versatility of the soil, the addition of the SCB-HW carbon-based material can significantly restore and promote the versatility of the soil damaged by invasion compared with the treatment group (CK) without the carbon-based material. Compared with SCB-LW, the SCB-HW has better effect in restoring soil multifunctionality, mainly due to the optimized physical and chemical structure, the higher-temperature hydrothermal reaction at 260 ℃ remarkably promotes the development of pores of the material, a developed mesoporous-macroporous hierarchical structure and a high specific surface area are formed (the specific surface area of the carbon-based material formed by the hydrothermal carbonization at 260 ℃ is 17.48m 2/g, and the specific surface area of the carbon-based material formed by the hydrothermal carbonization at 180 ℃ is 3.10m 2/g), so that the adsorption capacity of residual sense substances of invasive plants is greatly enhanced, the biotoxicity of the residual sense substances is reduced, a richer perching space is provided for beneficial microorganisms, and the recovery of the diversity of microbial communities and key metabolic activities (such as nutrient circulating enzymes) is effectively promoted. Meanwhile, the activation degree of mineral components (such as potassium and silicon) in ash at the temperature is higher, so that the effective slow release of nutrients and synergistic passivation of potential pollutants can be realized, and the directional evolution of surface functional groups (such as the formation of stable quinone groups) jointly optimizes the soil microenvironment and more effectively reverses the soil structural damage (the improvement of the stability of aggregates), the biological activity inhibition and the nutrient circulation disorder caused by invasion.|[0089] In terms of improving the carbon fixation capacity of soil, compared with a treatment group without adding the carbon-based material, the addition of the SCB-HW and the SCB-LW carbon-based materials can obviously improve the carbon fixation index of the soil damaged by invasion, but the improvement effect of the SCB-HW carbon-based material (the carbon fixation index of the soil is 0.70) is better than that of the SCB-LW carbon-based material (the carbon fixation index of the soil is 0.61). The SCB-HW is obviously superior to SCB-LW in improving the carbon holding capacity of soil, and has the core that the high-stability and strengthening stabilization effect of a carbon skeleton is that the high-temperature hydrothermal reaction depth of 260 ℃ promotes the aromatic polycondensation reaction of raw materials, a stable sp2 carbon network which has higher polymerization degree and is rich in condensed ring aromatic structures is formed, the biodegradability of the material is obviously enhanced, and the material directly contributes to long-term carbon fixation as a durable carbon warehouse. In addition, the surface chemical characteristics (such as moderate hydrophobicity and stable quinolyl) evolving at the temperature can more efficiently interact with soil organic matters through pi-pi action, hydrogen bonds and possible covalent bonding mechanisms, so that the physical migration and biomineralization loss of active carbon components are effectively reduced, and the chemical protection and stabilization capability of original and newly added organic carbon of the soil is greatly improved.|[0090] Effect example 1 shows that the application effect of the solidago canadensis stalk hydrothermal carbon-based material prepared at 260 ℃ is better than that of the solidago canadensis stalk hydrothermal carbon-based material prepared at 180 ℃.|[0091] Effect example 2|[0092] And (3) measuring and analyzing the improvement performance of the carbon-based materials SCB-HW prepared in the step (2) of the embodiment 1 and the improvement performance of the carbon-based materials SCB-HW4 and SCB-HW12 prepared in the proportion 2 on the multi-functional recovery and carbon retention capacity of the solidago canadensis invasion-induced soil. The soil multi-functional recovery and carbon retention were calculated in the same manner as in effect example 1.|[0093] The test procedure was the same as in effect example 1, and the potting experiment was divided into 4 treatments, namely, no carbon-based material treatment (CK) addition, SCB-HW carbon-based material treatment (SCB-HW) prepared in step (2) of example 1 addition, SCB-HW4 carbon-based material treatment (SCB-HW 4) prepared in comparative example 2 addition, and SCB-HW carbon-based material treatment (SCB-HW 12) prepared in comparative example 2 addition, each treatment being repeated 3 times. The experimental results are shown in Table 2.|[0094] TABLE 2 influence of carbon-based materials prepared in example 1 and comparative example 2 on soil versatility index and carbon fixation index due to foreign plant invasion|[0095] |[0096] Note that the tabular data is presented in the form of "mean ± standard deviation".|[0097] As can be seen from table 2, in terms of restoration of soil versatility, the addition of three carbon-based materials of SCB-HW, SCB-HW4 and SCB-HW12 all improved the versatility of the invading damage-induced soil to a different extent compared to the treatment group (CK) without carbon-based material, wherein the restoration effect of SCB-HW (soil multifunction index of 0.12) was most remarkable, SCB-HW12 times (0.08), and SCB-HW4 was minimally improved (0.04). The method has the advantages that the hydrothermal reaction time is prolonged to 8 hours at 260 ℃, the construction of the optimal pore structure and surface chemical characteristics of the soil function recovery are facilitated, when the hydrothermal time is only 4 hours, carbonization is insufficient, pores are not fully developed, the adsorption and passivation capability of the material to chemical sensing substances are limited, the improvement range of the soil multifunctionality is small, when the hydrothermal time is prolonged to 12 hours, although the aromaticity is further improved, excessive polycondensation is easy to cause partial pore collapse and pore diameter structure singleization, the number of oxygen-containing functional groups on the surface is reduced, the comprehensive regulation capability of the material to chemical sensing substances and nutrients is weakened, and the repair effect is superior to that of SCB-HW4, but is still lower than that of SCB-HW prepared under the condition of 8 hours.|[0098] In terms of improving the carbon fixation capacity of soil, compared with CK treatment, the addition of three carbon-based materials of SCB-HW4, SCB-HW12 and SCB-HW can improve the carbon fixation index of the invaded damaged soil, wherein the carbon fixation index of the SCB-HW is the highest (0.70), the carbon fixation index of the SCB-HW is the next 12 (0.67), and the carbon fixation index of the SCB-HW4 is the lowest (0.62). This shows that a better balance is achieved for the carbon skeleton formed at a hydrothermal reaction time of 8h at 260 ℃. On one hand, the 8h hydrothermal reaction can ensure sufficient aromatization polycondensation, and simultaneously, a proper amount of pore structures and a certain amount of oxygen-containing functional groups are reserved, so that the material has higher biodegradability, and can form a stable complex with soil organic matters in a pi-pi action, hydrogen bonds and other modes, thereby more effectively reducing migration and mineralization of active organic carbon, and on the other hand, a properly developed pore structure is beneficial to the organic carbon to be embedded and embedded, and the physical protection effect is enhanced. In contrast, the SCB-HW4 carbon network prepared under the condition of 4 hours is not perfect, the stable carbon proportion is lower, and the carbon fixation index is improved only to a limited extent, while the SCB-HW12 prepared under the condition of 12 hours has higher aromaticity, but excessive polycondensation and pore degradation weaken the physical-chemical synergistic protection capability on soil organic carbon, so that the carbon fixation index is higher than that of the SCB-HW4 but still not as high as that of the SCB-HW.|[0099] Effect example 2 shows that in the solidago canadensis straw hydro-thermal carbon-based material prepared under the condition of 260 ℃, the SCB-HW with the hydro-thermal reaction time of 8h is superior to the SCB-HW4 and the SCB-HW12 prepared under the conditions of 4h and 12h in terms of improving the versatility and carbon holding capacity of the invasion-induced damage soil, and the preferred hydro-thermal reaction time of 8h has obvious technical effect and is one of key parameters for realizing the best restoration and carbon fixing performance.|[0100] Effect example 3|[0101] The carbon-based materials SCB-HW and SCB-HN prepared in the example 1 were assayed and analyzed for the improvement of the recovery of the versatility and the carbon retention ability of the soil caused by invasion of Solidago canadensis. The soil multi-functional recovery and carbon retention were calculated in the same manner as in effect example 1.|[0102] The test procedure was the same as in effect example 1, except that the potting experiment was divided into 3 treatments, i.e., no carbon-based material treatment (CK) added, SCB-HN carbon-based material treatment (SCB-HN) prepared in example 1 added, and SCB-HW carbon-based material treatment (SCB-HW) prepared in step (2) of example 1 added, each treatment being repeated 3 times. The experimental results are shown in FIG. 1.|[0103] FIG. 1 is a graph showing the effect of adding the SCB-HW carbon-based material and the SCB-HN carbon-based material prepared in example 1 to soil on the versatility and carbon sequestration ability of the soil. As can be seen from fig. 1, in the aspect of restoring the soil versatility, the addition of both SCB-HN and SCB-HW carbon-based materials can significantly restore and enhance the versatility of the invading damage-induced soil, compared to the treatment group without adding the carbon-based material, but the restoration effect of SCB-HN carbon-based material (soil multifunction index of 0.69) is higher than that of SCB-HW carbon-based material (soil multifunction index of 0.12). Compared with SCB-HW, SCB-HN has better effect in restoring soil multifunctionality, and the core is the huge specific surface area and high dispersibility caused by the superfine particle size. The scale of the near nanometer grade endows SCB-HN carbon-based material with extremely high specific surface area and rich surface active sites, so that the SCB-HN carbon-based material can more efficiently and uniformly adsorb and passivate residual solidago canadensis allelopathy substances in soil, and the inhibition effect of the solidago canadensis on indigenous microorganisms and plants is remarkably reduced. Meanwhile, the ultrafine particles can penetrate into soil micropores and rhizosphere micro-domains, provide order-of-magnitude multiplication colonization sites for beneficial microorganisms, greatly promote reconstruction of microbial community diversity and recovery of key enzyme activities (such as dehydrogenase and phosphatase), and accelerate nutrient circulation processes. In addition, the compact network structure formed by the near-nanoscale particles in the soil can bridge soil particles more effectively and promote the formation of stable aggregates, so that the physical structure (ventilation and water retention) and biochemical functions of the soil are systematically improved. The SCB-HW carbon-based material is a millimeter-sized material, and has greatly limited adsorption capacity, microorganism carrier effect and structure improvement efficiency due to overlarge particle size, low specific surface area and poor dispersibility.|[0104] In terms of improving the carbon fixation capacity of soil, compared with a treatment group without adding the carbon-based material, the addition of the SCB-HN and the SCB-HW carbon-based materials can obviously improve the carbon fixation index of the soil damaged by invasion, but the improvement effect of the SCB-HN carbon-based material (the carbon fixation index of the soil is 0.77) is 10 percent higher than that of the SCB-HW carbon-based material (the carbon fixation index of the soil is 0.70). SCB-HN is obviously superior to SCB-HW in improving the carbon holding capacity of soil, and the key mechanism is the physical protection and chemical stabilization of the nano-scale reinforcement. The near-nano particles can be highly dispersed and tightly embedded into a soil matrix due to the extremely small size and the huge specific surface area, are particularly easy to enter the inside of an aggregate or combine with the surface of minerals to form a physical barrier, effectively wrap and protect active organic carbon components, reduce the contact of the active organic carbon components with microorganisms and enzymes, and reduce the mineralization rate. More importantly, the superfine particle size enables the superfine particle size to expose exponentially growing surface functional groups (such as carboxyl, phenolic hydroxyl and quinone groups), and the groups can be tightly combined with soil organic matter molecules through strong chemical adsorption (such as coordination bonds, hydrogen bonds and pi-pi actions) to form a stable organic-mineral-carbon complex, so that chemical bonding stabilization on original and newly added organic carbon of the soil is remarkably enhanced. The SCB-HW has small specific surface area, low surface activity and difficult effective dispersion to a soil micro-domain, has weak physical isolation effect, and has severely insufficient chemical bonding capability with soil organic matters, so that the SCB-HW has limited contribution to long-term stabilization of a carbon reservoir.|[0105] Effect example 3 shows that the application effect of the near-nanoscale solidago canadensis straw hydro-carbon-based material is better than that of the non-near-nanoscale solidago canadensis straw hydro-carbon-based material.|[0106] Effect example 4|[0107] The carbon-based materials SCB-HN and SCB-HN2 and SCB-HN12 prepared in the example 1 and the comparative example 3 are determined and analyzed to restore the multi-functionality of the soil and improve the carbon holding capacity caused by the invasion of solidago canadensis. The soil multi-functional recovery and carbon retention were calculated in the same manner as in effect example 1.|[0108] The test procedure was the same as in effect example 1, except that the potting experiment was divided into 4 treatments, namely, no carbon-based material treatment (CK), SCB-HN carbon-based material treatment (SCB-HN) prepared in example 1, SCB-HN2 carbon-based material treatment (SCB-HN 2) prepared in comparative example 3 and SCB-HN12 carbon-based material treatment (SCB-HN 12) prepared in comparative example 3, each treatment being repeated 3 times. The experimental results are shown in Table 3.|[0109] TABLE 3 influence of carbon-based materials prepared in example 1 and comparative example 3 on soil versatility index and carbon fixation index due to foreign plant invasion|[0110] |[0111] Note that the tabular data is presented in the form of "mean ± standard deviation".|[0112] As can be seen from table 3, there is a significant difference in the effect of the addition of three near-nanocarbon-based materials SCB-HN, SCB-HN2 and SCB-HN12 on the improvement of the versatility of the intrusion-induced soil, compared to the treatment group without the addition of the carbon-based material, in terms of restoration of the versatility of the soil. Among them, the recovery effect of SCB-HN treatment prepared by ball milling for 6 hours (soil versatility index of 0.69) is most remarkable, SCB-HN12 treatment is performed for a second time (0.62), while SCB-HN2 treatment prepared by ball milling for 2 hours cannot improve soil versatility, but rather exhibits negative shift (-0.59). This shows that ball milling time is one of the key parameters for regulating and controlling the functional effect of near-nano carbon based materials under the same raw materials and hydrothermal conditions. When the ball milling time is only 2 hours, the grain diameter refinement degree is limited, the increase of the specific surface area and the surface active site is not obvious, the material still keeps more coarse grain structures, the rhizosphere and the aggregate micro-domain are difficult to fully enter, the adsorption and passivation capability of chemical sensing substances are limited, and the functional microorganisms are difficult to provide enough colonization sites, even certain disturbance is generated to the soil micro-environment due to the problems of unstable grain diameter distribution, local aggregation and the like, so that the multifunction is not effectively recovered. In contrast, when the ball milling time is prolonged to 6 hours, the particle size of the material is reduced to be near nano-scale, the specific surface area and the exposure degree of the surface functional groups are obviously improved, particles can be more uniformly dispersed in soil micropores and rhizosphere areas, and efficiently adsorb and slowly release sensing substances, a large amount of microorganism adhesion and growth spaces are provided, and the comprehensive recovery of the physical and chemical properties, the microorganism diversity and the key enzyme activity of the soil is cooperatively promoted, so that the optimal effect is shown in the aspect of improving the multifunctionality. Further prolonging the ball milling time to 12h, while still keeping a higher multi-functional index (0.62), the repairing effect is lower than that of SCB-HN but better than that of SCB-HN2 because the long-time strong mechanical force is easy to cause collapse of partial pore structures, too fine particles to agglomerate and mechanical damage of surface functional groups, so that the material is slightly inferior to 6h treatment in the aspects of expanding microorganism habitat space and optimizing pore connectivity.|[0113] In terms of improving the carbon fixation capacity of soil, compared with CK treatment (the carbon fixation index of the soil is 0.52), the addition of three near-nano carbon-based materials of SCB-HN2, SCB-HN12 and SCB-HN can improve the carbon fixation index of the soil caused by invasion, wherein the improving effect of the SCB-HN is most prominent (the carbon fixation index of the soil is 0.77) and is remarkably higher than that of the SCB-HN12 (0.74) and the SCB-HN2 (0.68). This demonstrates that carbon stability can be optimized by combining 6h ball milling treatment on the basis of 260 ℃ hydrothermal carbonization. On one hand, moderate ball milling time is beneficial to breaking large particles and exposing more mesoporous-microporous structures and oxygen-containing functional groups, so that the carbon-based material can stabilize soil organic carbon in an aggregate or on the surface of minerals through a double way of physical embedding and chemical bonding (pi-pi action, hydrogen bonding and the like), and the synergistic effect of physical protection and chemical protection is enhanced, and on the other hand, the 6-hour ball milling can not excessively destroy an aromatic carbon network and key functional groups, so that the material self maintains higher biodegradability and the binding capability with soil organic matters. In contrast, SCB-HN2 prepared by 2h ball milling has limited effective surface sites capable of participating in physical-chemical stabilization of organic carbon due to insufficient grain size refinement and insufficient development of pore structure, and SCB-HN12 prepared by 12h ball milling has smaller lifting amplitude of carbon fixation index, while partial micropores-mesopores are compacted or collapsed due to long-time mechanical action although the grain size is finer, and surface functional groups are subjected to a certain degree of shearing damage, so that the surface functional groups are slightly inferior to SCB-HN in long-term carbon stabilization.|[0114] Effect example 4 shows that under the same raw materials and hydrothermal conditions, the near nanoscale Solidago canadensis straw carbon-based material SCB-HN prepared by ball milling time of 6h is superior to SCB-HN2 and SCB-HN12 prepared under the ball milling conditions of 2h and 12h in terms of improving the multifunctionality and carbon holding capacity of the invasion-induced soil, and the preferential 6h ball milling modification time of the invention has remarkable technical effects and is one of key parameters for realizing optimal restoration and carbon fixing performance of the carbon-based material.|[0115] Effect example 5|[0116] The carbon-based materials SCB-HN, CB-HN and PB-HN prepared in the examples 1, 4 and 5 were analyzed for the improvement of the multi-functional recovery and carbon retention ability of the solidago canadensis invasion-induced soil. The soil multi-functional recovery and carbon retention were calculated in the same manner as in effect example 1.|[0117] The test procedure was the same as in effect example 1, except that the potting experiment was divided into 4 treatments, namely, no carbon-based material treatment (CK), SCB-HN carbon-based material treatment (SCB-HN) prepared in example 1, CB-HN carbon-based material treatment (CB-HN) prepared in comparative example 4 and PB-HN carbon-based material treatment (PB-HN) prepared in comparative example 5, each treatment being repeated 3 times. The experimental results are shown in FIG. 2.|[0118] FIG. 2 is a graph showing the effect of adding the SCB-HN carbon-based material prepared in example 1, the CB-HN carbon-based material prepared in comparative example 4, and the PB-HN carbon-based material prepared in comparative example 5 to soil, on the versatility and carbon fixing ability of the soil. As can be seen from fig. 2, in the aspect of restoring the soil versatility, the addition of SCB-HN and CB-HN carbon-based materials can significantly restore and enhance the versatility of the invasion-induced soil, compared to the treatment group without carbon-based materials, wherein the effect of SCB-HN is most prominent (soil versatility index of 0.69) and significantly higher than CB-HN (soil versatility index of 0.14) and PB-HN (soil versatility index of-0.28). SCB-HN (Solidago canadensis straw carbon-based material) has better effect in restoring soil versatility compared with CB-HN (corn straw carbon-based material) and PB-HN (peach branch carbon-based material), and is characterized in that the special ash composition and pore structure of the raw materials. The solidago canadensis straw is rich in silicon, potassium and trace metal elements, forms high-activity amorphous silicate and mineral phases in ash of derived carbon, can efficiently adsorb and passivate residual homologous sense substances in soil, lightens the inhibition of the homologous sense substances to microbial communities, and meanwhile, the fiber structure of the raw material forms a developed mesopore-micropore hierarchical system after carbonization, so that the retention capacity of moisture and nutrients and microbial habitat space are remarkably improved, and the stability and biological activity recovery of aggregates of damaged soil are pertinently promoted. The corn straw carbon-based material is low in ash content and insufficient in pore uniformity, and peach branch carbon-based material is dominant in macropores and limited in specific surface area due to lignin derivative, so that the equivalent removal of chemical substances and the synergistic restoration of micro ecology are difficult to realize.|[0119] In terms of improving the carbon fixation capacity of the soil, compared with a treatment group without adding the carbon-based material, the addition of the SCB-HN, CB-HN and PB-HN carbon-based materials can improve the carbon fixation index of the invaded damaged soil, wherein the effect of the SCB-HN is most prominent (the carbon fixation index of the soil is 0.77) and is obviously higher than that of the CB-HN (the carbon fixation index of the soil is 0.67) and the PB-HN (the carbon fixation index of the soil is 0.56). The advantage of SCB-HN in carbon holding capacity is derived from a double stabilization mechanism given by raw materials, namely the high silicon characteristic of the solidago canadensis straw promotes the formation of a silicon-carbon composite skeleton in carbon, a siliceous coating layer effectively insulates microbial attack and greatly improves the stability of the carbon, and meanwhile, the specific proportion of lignin/cellulose in the raw materials is carbonized to generate a high proportion fused ring aromatic structure and surface quinolyl groups, so that soil organic matters can be strongly fixed through chemical bonding (such as Si-O-C covalent bonds and quinone-phenol redox couples) to form an anti-degradation organic-mineral complex. In contrast, the low-carbonization aromatic structure of the corn straw carbon-based material CB-HN is easy to mineralize, the peach branch carbon-based material PB-HN has strong hydrophobicity but sparse bonding sites, and the contribution of the low-carbonization aromatic structure to the long-term stability of the soil carbon reservoir is obviously weaker than that of the SCB-HN.|[0120] Effect example 5 shows that under the same preparation conditions, the application effect of the carbon-based material prepared by taking solidago canadensis as a raw material is better than that of the carbon-based material prepared by taking corn stalks and peach branches as raw materials.|[0121] The experimental results of comprehensive effect examples 1-5 show that the carbon-based material (SCB-HN) prepared by taking solidago canadensis as a raw material and modifying the solidago canadensis through combining the hydrothermal carbonization at 260 ℃ and the near-nanoscale grinding for 6 hours has the best effect of restoring the multifunctionality of the soil and improving the carbon holding capacity caused by the invasion of solidago canadensis.|[0122] The present invention is not limited to the above-mentioned embodiments, and any changes or substitutions that can be easily understood by those skilled in the art within the technical scope of the present invention are intended to be included in the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope of the claims. Family Number|(117637004)|117637004|Abstract|(CN121426099 A)|The invention discloses a near - nano carbon - based material for function recovery and carbon fixation capability improvement of alien plant invasion damaged soil and a preparation method of the near - nano carbon - based material , and belongs to the technical field of soil remediation and carbon fixation and sink increase . The near - nano carbon - based material is prepared by the following steps : by taking an external invasive plant Canadian yellow flower stalk as a raw material , crushing , screening , mixing with water , carrying out hydrothermal reaction to obtain a hydrothermal carbonization product , and carrying out ball milling and screening treatment to obtain the near - nano carbon - based material . The obtained near - nano carbon - based material has a high - aromaticity carbon skeleton , a rich mesoporous - macroporous structure and a relatively high amorphous silicon content , can efficiently adsorb and passivate residual allelochemicals of solidago canadensis , reconstruct an aggregate structure , promote microbial diversity and key enzyme activity recovery , strengthen organic carbon - mineral bonding and improve the stability of the material . Therefore , invasion - induced multifunctional soil degradation is accurately reversed , and in - situ remediation of the soil structure and function and improvement of the carbon immobilization capacity are achieved . Experimental results show that the carbon - based material provided by the invention can increase the multifunctional index of invasion - induced damaged soil by about 560% and increase the carbon sequestration index by about 48.1%. |IPC codes|(CN121426099 A)|B01J - 020/20 |B01J - 020/28 |B01J - 020/30 |C01B - 032/15 | Basic materials chemistry|Chemical engineering|Environmental technology|Materials, metallurgy B01J-020/06|B01J-020/12|B01J-020/20|B01J-020/22|B01J-020/24|B01J-020/28/004|B01J-020/28/009|B01J-020/30/78|B01J-2220/4806|B01J-2220/4825|B01J-2220/485|B01J-2220/4887|B09C-001/00|B09C-001/00/2|B09C-001/08|B09C-2101/00|C01B-032/05|C01B-032/15|C09K-017/02 B01J-020/06|B01J-020/12|B01J-020/20|B01J-020/22|B01J-020/24|B01J-020/28/004|B01J-020/28/009|B01J-020/30/78|B01J-2220/4806|B01J-2220/4825|B01J-2220/485|B01J-2220/4887|B09C-001/00|B09C-001/00/2|B09C-001/08|B09C-2101/00|C01B-032/05|C01B-032/15|C09K-017/02 B01J-020/20|B01J-020/28|B01J-020/30|B09C-001/00|C01B-032/15|C09K-017/02 B01J-020/20|B01J-020/28|B01J-020/30|B09C-001/00|C01B-032/15|C09K-017/02 PENDING (CN121426099)|PENDING ALIVE (CN121426099)|ALIVE (CN121426099)|LEGAL DETAILS FOR CN121426099|Actual or expected expiration date=2045-11-28|Legal state=ALIVE|Status=PENDING|Event publication date=2025-11-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511768705|Application date=2025-11-28|Standardized application number=2025CN-1768705|Event publication date=2026-01-30|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121426099|Publication stage code=A|Publication date=2026-01-30|Standardized publication number=CN121426099|Event publication date=2026-01-30|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2026-02-17|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121426099)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKeYQdI+TTq9Mlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080695671&ekey=1907&xpn=CN121426099&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=rg55fKlZBQuHUV9yeNAUp5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121426099)|CN (CN121426099)|NAME=JIANGSU UNIVERSITY , COUNTRY=CN (CN121426099)|NAME=AN RAN;BEIJING SHENGGUANGXINHE IP FIRM , REG=16117 (CN121426099)|NAME=LI GUANLIN|NAME=ZHAO XIN|NAME=ZHANG QIUYUE|NAME=HU JIAN|NAME=WANG CHEN|NAME=LOU JIABAO|NAME=WANG YANJIAO|NAME=ZHENG XIAOJUN|NAME=CHEN XUNFENG|NAME=XIAO WENYA|NAME=DU DAOLIN 0 1 Titre: (CN121426099)|Near-nano carbon-based material for recovering function and improving carbon fixation capacity of alien plant invasion damaged soil and preparation method thereof Résumé: (CN121426099)|The invention discloses a near-nano carbon-based material for function recovery and carbon fixation capability improvement of alien plant invasion damaged soil and a preparation method of the near-nano carbon-based material, and belongs to the technical field of soil remediation and carbon fixation and sink increase. The near-nano carbon-based material is prepared by the following steps: by taking an external invasive plant Canadian yellow flower stalk as a raw material, crushing, screening, mixing with water, carrying out hydrothermal reaction to obtain a hydrothermal carbonization product, and carrying out ball milling and screening treatment to obtain the near-nano carbon-based material. The obtained near-nano carbon-based material has a high-aromaticity carbon skeleton, a rich mesoporous-macroporous structure and a relatively high amorphous silicon content, can efficiently adsorb and passivate residual allelochemicals of solidago canadensis, reconstruct an aggregate structure, promote microbial diversity and key enzyme activity recovery, strengthen organic carbon-mineral bonding and improve the stability of the material. Therefore, invasion-induced multifunctional soil degradation is accurately reversed, and in-situ remediation of the soil structure and function and improvement of the carbon immobilization capacity are achieved. Experimental results show that the carbon-based material provided by the invention can increase the multifunctional index of invasion-induced damaged soil by about 560% and increase the carbon sequestration index by about 48.1%. 108 Abstract gpt-4o-mini no The article focuses on a carbon-based material for soil remediation and carbon fixation but does not involve accelerated weathering of minerals or CO₂ capture through mineral carbonation.
111 CN202122978429U CN202122978429U CN217431790 101804733 CN217431790 U 2022-09-16 [CN217431790U] 2021-11-30 2021-11-30 2022-09-16 (CN217431790U)|2022-09-16 (CN217431790)|2031-11-30 (CN217431790)|Magnetic residue screening device for cleaning carbon black (CN217431790)|The utility model discloses a carbon black cleaning magnetic residue screening device which comprises a powder tank, a smashed metal collecting structure is installed on the inner side of the powder tank, and a flow dividing structure is installed at the bottom end of the powder tank. The crushed metal collecting structure comprises a plurality of stirring shaft pipes, a plurality of crushing rollers, a plurality of crushing blocks, a plurality of crushing chain wheels, a pair of crushing drivers, a pair of crushing chains, a plurality of electromagnetic iron rods, a plurality of inner bearing blocks, a plurality of outer bearing blocks and a side wall supporting frame. The utility model relates to the technical field of carbon black iron removal, a powder tank stirring device is changed into a magnetic stirring device, iron impurities in powdery carbon black can be fully adsorbed, when the machine is shut down each time, powder at the bottom of a powder tank is empty, an electromagnetic device is closed, and iron adsorbable magnetic substances fall off. And magnetic substances are cleaned from the cleaning port to achieve the purposes of reducing washing screen residues and improving the purity of the carbon black. HANCHENG HEIMAO CARTON BLACK (CN217431790)|HANCHENG HEIMAO CARTON BLACK CO., LTD. ([CN]) MA LIPENG|CHEN ZHIFENG|FENG YANLONG|LI YONGHONG|SHI XIANGPENG (CN217431790)|MA LIPENG|CHEN ZHIFENG|FENG YANLONG|LI YONGHONG|SHI XIANGPENG (CN217431790)|HUANG DEYUE;BEIJING RAINBOW XINGYUAN INTELLECTUAL PROPERTY LAW FIRM|Reg. Nb: 11297 (CN217431790)|After the carbon black is granulated, the magnetic impurities are wrapped in the carbon black particles, the total mass is increased due to the thick attaching layer, and partial magnetic impurity particles are difficult to separate by magnetic separation.| (CN217431790)|1. A device for cleaning magnetic screen remnants by carbon black comprises a powder tank and a magnetic screen remnants cleaning device, wherein the powder tank is characterized in that a crushed metal collecting structure is arranged on the inner side of the powder tank, and a shunting structure is arranged at the bottom end of the powder tank; the crushed metal collecting structure comprises a plurality of stirring shaft tubes, a plurality of crushing rollers, a plurality of crushing blocks, a plurality of crushing chain wheels, a pair of crushing driving machines, a pair of crushing chains, a plurality of electromagnet rods, a plurality of inner bearing blocks, a plurality of outer bearing blocks and a side wall supporting frame; the utility model discloses a crushing driving machine, including lateral wall support frame, a plurality of, crushing driving machine, a plurality of, crushing sprocket install respectively in a plurality of on the powder jar, the lateral wall support frame install in on the lateral wall of powder jar, a plurality of respectively through a plurality of outer bearing piece install in the lateral wall support frame and on the powder jar, a plurality of crushing cylinder install respectively in a plurality of on the stirring central tube, a plurality of crushing piece install respectively in a plurality of crushing cylinder and the inboard of powder jar, a plurality of the electromagnetism iron pole is respectively through a plurality of interior bearing piece install in a plurality of the inboard of stirring central tube, it is a pair of crushing driving machine install in on the powder jar, a plurality of crushing sprocket installs respectively in a plurality of stirring central tube and a pair of on the drive end of crushing driving machine, it is a pair of crushing chain suit in a plurality of on the crushing sprocket.| (CN217431790)|The utility model discloses a carbon black cleaning magnetic screen residue device, which comprises a powder tank, wherein a crushed metal collecting structure is arranged at the inner side of the powder tank, and a shunting structure is arranged at the bottom end of the powder tank; the crushed metal collecting structure comprises: the crushing device comprises a plurality of stirring shaft tubes, a plurality of crushing rollers, a plurality of crushing blocks, a plurality of crushing chain wheels, a pair of crushing driving machines, a pair of crushing chains, a plurality of electromagnet rods, a plurality of inner bearing blocks, a plurality of outer bearing blocks and a side wall supporting frame; the utility model relates to a carbon black deironing technical field changes powder jar agitating unit into the magnetic stirring, can fully adsorb iron class impurity in the likepowder carbon black, when shutting down at every turn, draws empty powder tank bottoms portion powder, closes electromagnetic means, and the adsorbable magnetic substance of iron class drops, clears up the magnetic substance from the clearance mouth in order to reach the purpose that reduces washing screen residue and improve carbon black purity.| (CN217431790)|CARBON BLACK(100,34)|POWDER TANK(100,23)|CARBON BLACK CLEARANCE MAGNETISM(100,5)|CLEARANCE MAGNETISM(100,5)|CLEANING MAGNETIC SCREEN REMNANT(100,1)|CRUSHING SPROCKET(98,7)|CRUSHING DRIVING MACHINE(90,10)|POWDER JAR(83,25)|ADSORBABLE MAGNETIC SUBSTANCE(77,1)|CRUSHING(72,19)|ELECTROMAGNETISM IRON POLE(72,2)|CRUSHING ROLLER(66,14)|IRON CLASS IMPURITY(65,1)|ELECTROMAGNET ROD(64,6)|MAGNETIC SCREEN RESIDUE(64,5)|MAGNETIC SCREEN REMNANT(61,1)|SCREEN RESIDUE(60,5)|CRUSHING CHAIN(59,5)|CRUSHED METAL(53,7)|CRUSHING BLOCK(52,3)|IRON CLASS DROP(49,1)|BIDIRECTIONAL ELECTROMAGNET STRIP(48,2)|MAGNETIC STIRRING(46,1)|CRUSHED PIECE(45,2)|STIRRING CENTRAL TUBE(43,6)|CARBON BLACK CLEANING(38,5)|CARBON BLACK DEIRONING(38,2)|STIRRING SHAFT TUBE(37,11)|SHUNTING STRUCTURE(36,4)|MAGNETIC SUBSTANCE(36,2)|MAGNETIC IMPURITY PARTICLE(32,1)|SHUNT SHAFT(29,8)|INTERIOR BEARING PIECE(29,2)|ROTATING WHEEL(27,7)|MAGNETIC DRAINAGE ROD(27,3)|FOLDING BAFFLE PLATE(27,2)|SHUNTING SHAFT(27,1)|CARBON BLACK PURITY(25,2)|SHUNT PLATE(24,4)|CARBON BLACK PARTICLE(24,1)|DRAW(24,1)|POWDER JAR LATERAL WALL(23,3)|DRIVING MACHINE(23,2)|CLEANING MAGNETIC SCREEN RESIDUE(22,3)|DRAINAGE VALVE(22,3)|POWDER CARBON BLACK(22,2)|MAGNETIC IMPURITY(21,5)|OUTER BEARING PIECE(21,2)|SHUNTING PLATE(21,1)|TOTAL MASS(19,1)|LATERAL WALL(18,11)|CONCAVE BEARING BLOCK(17,10)|SUIT(16,3)|SUPPORTING FRAME(16,3)|Y SHAPED SHUNT TUBE(15,12)|INNER BEARING BLOCK(15,5)|FLEXIBLE DRAINAGE TUBE(15,3)|Y SHAPED SHUNTING PIPE(14,1)|OUTER BEARING BLOCK(13,5)|PORTION POWDER(13,1)|SUPPORT FRAME(12,9)|DRIVER PULVERIZATION(12,3)|MAGNETIC SEPARATION(11,2)|Y SHAPED SHUNT PIPE(10,3)|SHUNT DRIVING RIGHT ANGLE(10,1)|BIDIRECTIONAL ELECTROMAGNET BAR(9,1)|MAGNETIC SUBSTANCE ADSORBED IMPURITY(9,1)|SMASH SPROCKET(9,1)|LATERAL WALL SUPPORT FRAME(8,8)|POWDER TANK JOINT(8,2)|ELECTROMAGNET POLE(8,1)|IMPURITY ADSORPTION(8,1)|NONEXCLUSIVE INCLUSION(8,1)|SPROCKET PULVERIZATION(8,1)|SURPLUS THING(8,1)|POWDERED CARBON BLACK(7,4)|STIRRING CENTRAL(7,4)|SMASH DRIVING MACHINE(7,2)|SQUARE SHAPED GATHERING BLOCK(7,2)|DRIVING RIGHT ANGLE PORT(7,1)|FERROMAGNETIC SUBSTANCE(7,1)|FOLDING SHUTTER(7,1)|EQUIPMENT OXIDATION ABRASION(6,1)|SMASH CHAIN(6,1)|EMPTY POWDER(4,1)|POWDER CONTAINER(4,1)| (CN217431790)|1. A device for cleaning magnetic screen remnants by carbon black comprises a powder tank and a magnetic screen remnants cleaning device, wherein the powder tank is characterized in that a crushed metal collecting structure is arranged on the inner side of the powder tank, and a shunting structure is arranged at the bottom end of the powder tank;|the crushed metal collecting structure comprises a plurality of stirring shaft tubes, a plurality of crushing rollers, a plurality of crushing blocks, a plurality of crushing chain wheels, a pair of crushing driving machines, a pair of crushing chains, a plurality of electromagnet rods, a plurality of inner bearing blocks, a plurality of outer bearing blocks and a side wall supporting frame;|the utility model discloses a crushing driving machine, including lateral wall support frame, a plurality of, crushing driving machine, a plurality of, crushing sprocket install respectively in a plurality of on the powder jar, the lateral wall support frame install in on the lateral wall of powder jar, a plurality of respectively through a plurality of outer bearing piece install in the lateral wall support frame and on the powder jar, a plurality of crushing cylinder install respectively in a plurality of on the stirring central tube, a plurality of crushing piece install respectively in a plurality of crushing cylinder and the inboard of powder jar, a plurality of the electromagnetism iron pole is respectively through a plurality of interior bearing piece install in a plurality of the inboard of stirring central tube, it is a pair of crushing driving machine install in on the powder jar, a plurality of crushing sprocket installs respectively in a plurality of stirring central tube and a pair of on the drive end of crushing driving machine, it is a pair of crushing chain suit in a plurality of on the crushing sprocket.|2. The device for cleaning magnetic screen residue by carbon black according to claim 1, wherein the shunting structure comprises a Y-shaped shunting pipe, a shunting shaft, a shunting plate, a pair of two-way electromagnet bars, a magnet bar, a plurality of concave bearing blocks, a plurality of rotating shafts, a plurality of rotating wheels and two pairs of folding shielding plates;|the Y-shaped shunt tube is installed on the bottom end of the powder tank, the shunt shaft is inserted into the inner side of the Y-shaped shunt tube, the shunt plate is installed on the shunt shaft, a shunt driving right-angle port is formed in the Y-shaped shunt tube, a pair of bidirectional electromagnet strips is installed on the shunt driving right-angle port in a pair respectively, magnet strips are installed on the shunt plate, a plurality of concave bearing blocks are installed on the two sides of the shunt plate respectively, a plurality of rotating shafts are installed on the concave bearing blocks respectively, a plurality of rotating wheels are installed on the rotating shafts respectively, two pairs of folding baffle plates are installed on the two sides of the shunt plate respectively, and two pairs of folding baffle plates are connected to the inner side of the powder tank respectively.|3. The carbon black cleaning magnetic screen residue device according to claim 2, wherein a drainage valve is arranged at the connection position of the powder tank and the Y-shaped shunt pipe.|4. The apparatus according to claim 2, wherein a pair of flexible drainage tubes are disposed on the Y-shaped shunt tube.|5. The carbon black cleaning magnetic screen residue device according to claim 1, wherein a plurality of the square-shaped gathering blocks are respectively arranged on the inner sides of the powder tanks.|6. The carbon black cleaning magnetic screen residue device as claimed in claim 1, wherein a plurality of magnetic drainage rods are respectively arranged on the inner sides of a plurality of the crushing rollers. (CN217431790)|TECHNICAL FIELD|[0001] The utility model relates to a carbon black deironing technical field specifically is a carbon black clearance magnetism screen surplus thing device.|BACKGROUND ART|[0002] A process for preparing carbon black includes such steps as generating powdered carbon black by incomplete combustion and cracking of hydrocarbon compound in reactor, conveying it to granulating system, drying in drier, conveying it to back system, removing impurities by the first device at the inlet of LO502 cage, the second device at the inlet of LO504 cage, the third device, and the automatic magnetic cleaning unit on feeding tube. In the production process, the powdered carbon black does not have any magnetic impurity adsorbable device before granulation. At present, the existing device for removing the magnetic impurities of the carbon black can only remove the easily adsorbed impurities of the magnetic substances such as oxidation abrasion of equipment after the carbon black is granulated. After the carbon black is granulated, the magnetic impurities are wrapped in the carbon black particles, the total mass is increased due to the thick attaching layer, and partial magnetic impurity particles are difficult to separate by magnetic separation. Obviously, a magnetic separation procedure for the powdered carbon black is added in the production process of the carbon black to remove magnetic impurities in the powdered carbon black as much as possible, so that the magnetic separation method plays a positive role in reducing screen residues and improving the purity of products, and in view of the above, the present invention is developed in order to deeply research the problems.|DISCLOSURE|SUMMERY OF THE UTILITY MODEL|[0003] Not enough to prior art, the utility model provides a carbon black clearance magnetism sieve surplus device has solved current partial background technical problem.|[0004] In order to achieve the above purpose, the utility model discloses a following technical scheme realizes: a carbon black cleaning magnetic screen residue device comprises: the powder tank is characterized in that a crushed metal collecting structure is arranged on the inner side of the powder tank, and a shunting structure is arranged at the bottom end of the powder tank;|[0005] the crushed metal collecting structure comprises: the crushing device comprises a plurality of stirring shaft tubes, a plurality of crushing rollers, a plurality of crushing blocks, a plurality of crushing chain wheels, a pair of crushing driving machines, a pair of crushing chains, a plurality of electromagnet rods, a plurality of inner bearing blocks, a plurality of outer bearing blocks and a side wall supporting frame;|[0006] the utility model discloses a crushing driving machine, including lateral wall support frame, a plurality of, crushing driving machine, a plurality of, crushing sprocket install respectively in a plurality of on the powder jar, the lateral wall support frame install in on the lateral wall of powder jar, a plurality of respectively through a plurality of outer bearing piece install in the lateral wall support frame and on the powder jar, a plurality of crushing cylinder install respectively in a plurality of on the stirring central tube, a plurality of crushing piece install respectively in a plurality of crushing cylinder and the inboard of powder jar, a plurality of the electromagnetism iron pole is respectively through a plurality of interior bearing piece install in a plurality of the inboard of stirring central tube, it is a pair of crushing driving machine install in on the powder jar, a plurality of crushing sprocket installs respectively in a plurality of stirring central tube and a pair of on the drive end of crushing driving machine, it is a pair of crushing chain suit in a plurality of on the crushing sprocket.|[0007] Preferably, the flow dividing structure includes: the device comprises a Y-shaped shunt pipe, a shunt shaft, a shunt plate, a pair of two-way electromagnet bars, a magnet bar, a plurality of concave bearing blocks, a plurality of rotating shafts, a plurality of rotating wheels and two pairs of folding shielding plates;|[0008] the powder jar comprises a powder jar, a powder distribution plate, a Y-shaped shunt tube, a shunt shaft, a pair of bidirectional electromagnet strips, a magnet strip, a plurality of concave bearing blocks, a plurality of rotary shafts, a plurality of rotary wheels, a plurality of folding type baffle plates and a plurality of powder cans, wherein the powder jar is provided with the powder jar, the powder jar is provided with the powder jar, the powder jar is provided with the powder jar, the powder is provided with the powder jar, the powder is provided with the powder jar, the powder is provided with the powder jar on the powder jar, a plurality of the powder is provided with the rotating axis, a plurality of Y, the rotating axis, a plurality of.|[0009] Preferably, a drainage valve is arranged at the joint of the powder tank and the Y-shaped shunt pipe.|[0010] Preferably, a pair of flexible drainage tubes are arranged on the Y-shaped shunt tube.|[0011] Preferably, the inner sides of the powder tanks are respectively provided with a plurality of clip-shaped gathering blocks.|[0012] Preferably, a plurality of magnetic drainage rods are respectively arranged on the inner sides of the plurality of crushing rollers.|[0013] The utility model provides a carbon black clearance magnetism sieve excess device. The method has the following beneficial effects: this carbon black clearance magnetism sieve excess device changes powder jar agitating unit into has magnetic agitating unit, can fully adsorb the interior ferromagnetic type impurity of likepowder carbon black, when shutting down at every turn, draws empty powder jar bottom powder, closes electromagnetic means, and the adsorbate of magnetism type drops, clears up ferromagnetic substance from the clearance mouth in order to reach the purpose that reduces washing sieve excess and improve carbon black purity.|DRAWINGS DESCRIPTION|[0014] Fig. 1 is a schematic front sectional view of a device for cleaning magnetic screen residue by carbon black of the present invention.|[0015] Fig. 2 is a schematic side view and sectional view of the device for cleaning magnetic screen residue by carbon black of the present invention.|[0016] Fig. 3 is an enlarged view of a portion "a" in fig. 1.|[0017] In the figure: 1. a powder tank; 2. a stirring shaft tube; 3. a crushing roller; 4. crushing the blocks; 5. a crushing sprocket; 6. a pulverizing driver; 7. crushing chains; 8. an electromagnet rod; 9. an inner bearing block; 10. an outer bearing block; 11. a sidewall support frame; 12. a Y-shaped shunt tube; 13. a shunt shaft; 14. a flow distribution plate; 15. a bidirectional electromagnet bar; 16. a magnet bar; 17. a concave bearing block; 18. a rotating shaft; 19. a rotating wheel; 20. a folding shutter.|INVENTION MODE|Detailed Description|[0018] The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.|[0019] Example 1|[0020] As shown in fig. 1-3, a pulverized metal collecting structure is installed inside the powder tank 1, and a flow dividing structure is installed at the bottom end of the powder tank 1;|[0021] specifically, the crushed metal collecting structure comprises: the crushing device comprises a plurality of stirring shaft tubes 2, a plurality of crushing rollers 3, a plurality of crushing blocks 4, a plurality of crushing chain wheels 5, a pair of crushing driving machines 6, a pair of crushing chains 7, a plurality of electromagnet rods 8, a plurality of inner bearing blocks 9, a plurality of outer bearing blocks 10 and a side wall support frame 11;|[0022] specifically, the lateral wall support frame 11 install in on the lateral wall of powder jar 1, a plurality of stirring central siphon 2 install in through a plurality of outer bearing piece 10 respectively in lateral wall support frame 11 and on the powder jar 1, a plurality of crushing roller 3 installs respectively in a plurality of on the stirring central siphon 2, a plurality of crushing piece 4 installs respectively in a plurality of crushing roller 3 and the inboard of powder jar 1, a plurality of electromagnet pole 8 installs respectively in a plurality of through a plurality of inner bearing piece 9 the inboard of stirring central siphon 2, it is a pair of smash driving machine 6 install in on the powder jar 1, a plurality of smash sprocket 5 install respectively in a plurality of stirring central siphon 2 and a pair of on the drive end of smash driving machine 6, it is a pair of smash chain 7 suit in a plurality of smash on the sprocket 5.|[0023] In the above, by pouring the raw material into the powder container 1 and operating the pair of pulverizing drivers 6, the pulverizing sprockets 5 on the driving ends of the pair of pulverizing drivers 6 are rotated, the crushing chain wheels 7 are respectively driven by a pair of crushing chain wheels 5, a plurality of crushing chain wheels 5 are respectively driven by a pair of crushing chain wheels 7 to rotate, the stirring shaft tubes 2 on the crushing chain wheels 5 are respectively driven by the crushing chain wheels, the crushing rollers 3 on the stirring shaft tubes 2 are respectively driven by the stirring shaft tubes 2, meanwhile, a plurality of electromagnet rods 8 in a plurality of stirring shaft tubes 2 magnetize a plurality of stirring shaft tubes 2 and the crushing rollers 3 on the stirring shaft tubes, so that a plurality of crushing rollers 3 and a plurality of crushing blocks 4 on the crushing rollers, the carbon black is crushed by a plurality of crushing blocks 4 which relatively rotate, and the iron metal component in the crushed carbon black is magnetically adsorbed.|[0024] Example 2|[0025] As shown in fig. 1-2, the shunting structure comprises: the device comprises a Y-shaped shunt pipe 12, a shunt shaft 13, a shunt plate 14, a pair of bidirectional electromagnet bars 15, magnet bars 16, a plurality of concave bearing blocks 17, a plurality of rotating shafts 18, a plurality of rotating wheels 19 and two pairs of folding shielding plates 20;|[0026] specifically, the Y-shaped shunt tube 12 is installed at the bottom end of the powder tank 1, the shunt shaft 13 is inserted into the inner side of the Y-shaped shunt tube 12, the splitter plate 14 is mounted on the splitter shaft 13, a splitter driving right-angle opening is formed on the Y-shaped splitter 12, a pair of the bidirectional electromagnet bars 15 are respectively mounted on the pair of the splitter driving right-angle openings, the magnet strips 16 are mounted on the splitter plate 14, the concave bearing blocks 17 are mounted on two sides of the splitter plate 14, the rotating shafts 18 are mounted on the concave bearing blocks 17, the rotating wheels 19 are mounted on the rotating shafts 18, the two pairs of folding shielding plates 20 are mounted on two sides of the splitter plate 14, and the two pairs of folding shielding plates 20 are connected to the inner side of the powder tank 1.|[0027] It should be noted that, in the above description, the pulverized and sieved carbon black falls into the Y-shaped shunt tube 12, and the magnet bars 16 on the shunt plate 14 are attracted to one side of the pair of shunt drive right-angle openings by one of the pair of bidirectional electromagnet bars 15 operating in the forward direction and the other one operating in the reverse direction, and repelling and adsorbing, so that the shunt plate 14 rotates along the shunt shaft 13, so that carbon black powder and ferrous metal powder are separated from each other, the shunt plate 14 and the Y-shaped shunt tube 12 are side-sealed by the two pairs of folding shielding plates 20, and the shunt plate 14 can stably rotate in the Y-shaped shunt tube 12 by the cooperation of the plurality of rotating shafts 18 on the plurality of concave bearing blocks 17 and the rotating wheels 19 thereon.|[0028] Preferably, a drainage valve is arranged at the joint of the powder tank 1 and the Y-shaped shunt pipe 12.|[0029] Preferably, a pair of flexible drainage tubes are disposed on the Y-shaped shunt 12.|[0030] Preferably, a plurality of square-shaped gathering blocks are respectively arranged on the inner sides of the powder tanks 1.|[0031] Preferably, a plurality of magnetic drainage rods are respectively arranged on the inner sides of the plurality of crushing rollers 3.|[0032] It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation. The use of the phrase "comprising one of the elements does not exclude the presence of other like elements in the process, method, article, or apparatus that comprises the element.|[0033] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. (CN217431790)|TECHNICAL FIELD|[0001] The utility model relates to a carbon black deironing technical field specifically is a carbon black clearance magnetism screen surplus thing device.|BACKGROUND ART|[0002] A process for preparing carbon black includes such steps as generating powdered carbon black by incomplete combustion and cracking of hydrocarbon compound in reactor, conveying it to granulating system, drying in drier, conveying it to back system, removing impurities by the first device at the inlet of LO502 cage, the second device at the inlet of LO504 cage, the third device, and the automatic magnetic cleaning unit on feeding tube. In the production process, the powdered carbon black does not have any magnetic impurity adsorbable device before granulation. At present, the existing device for removing the magnetic impurities of the carbon black can only remove the easily adsorbed impurities of the magnetic substances such as oxidation abrasion of equipment after the carbon black is granulated. After the carbon black is granulated, the magnetic impurities are wrapped in the carbon black particles, the total mass is increased due to the thick attaching layer, and partial magnetic impurity particles are difficult to separate by magnetic separation. Obviously, a magnetic separation procedure for the powdered carbon black is added in the production process of the carbon black to remove magnetic impurities in the powdered carbon black as much as possible, so that the magnetic separation method plays a positive role in reducing screen residues and improving the purity of products, and in view of the above, the present invention is developed in order to deeply research the problems.|DISCLOSURE|SUMMERY OF THE UTILITY MODEL|[0003] Not enough to prior art, the utility model provides a carbon black clearance magnetism sieve surplus device has solved current partial background technical problem.|[0004] In order to achieve the above purpose, the utility model discloses a following technical scheme realizes: a carbon black cleaning magnetic screen residue device comprises: the powder tank is characterized in that a crushed metal collecting structure is arranged on the inner side of the powder tank, and a shunting structure is arranged at the bottom end of the powder tank;|[0005] the crushed metal collecting structure comprises: the crushing device comprises a plurality of stirring shaft tubes, a plurality of crushing rollers, a plurality of crushing blocks, a plurality of crushing chain wheels, a pair of crushing driving machines, a pair of crushing chains, a plurality of electromagnet rods, a plurality of inner bearing blocks, a plurality of outer bearing blocks and a side wall supporting frame;|[0006] the utility model discloses a crushing driving machine, including lateral wall support frame, a plurality of, crushing driving machine, a plurality of, crushing sprocket install respectively in a plurality of on the powder jar, the lateral wall support frame install in on the lateral wall of powder jar, a plurality of respectively through a plurality of outer bearing piece install in the lateral wall support frame and on the powder jar, a plurality of crushing cylinder install respectively in a plurality of on the stirring central tube, a plurality of crushing piece install respectively in a plurality of crushing cylinder and the inboard of powder jar, a plurality of the electromagnetism iron pole is respectively through a plurality of interior bearing piece install in a plurality of the inboard of stirring central tube, it is a pair of crushing driving machine install in on the powder jar, a plurality of crushing sprocket installs respectively in a plurality of stirring central tube and a pair of on the drive end of crushing driving machine, it is a pair of crushing chain suit in a plurality of on the crushing sprocket.|[0007] Preferably, the flow dividing structure includes: the device comprises a Y-shaped shunt pipe, a shunt shaft, a shunt plate, a pair of two-way electromagnet bars, a magnet bar, a plurality of concave bearing blocks, a plurality of rotating shafts, a plurality of rotating wheels and two pairs of folding shielding plates;|[0008] the powder jar comprises a powder jar, a powder distribution plate, a Y-shaped shunt tube, a shunt shaft, a pair of bidirectional electromagnet strips, a magnet strip, a plurality of concave bearing blocks, a plurality of rotary shafts, a plurality of rotary wheels, a plurality of folding type baffle plates and a plurality of powder cans, wherein the powder jar is provided with the powder jar, the powder jar is provided with the powder jar, the powder jar is provided with the powder jar, the powder is provided with the powder jar, the powder is provided with the powder jar, the powder is provided with the powder jar on the powder jar, a plurality of the powder is provided with the rotating axis, a plurality of Y, the rotating axis, a plurality of.|[0009] Preferably, a drainage valve is arranged at the joint of the powder tank and the Y-shaped shunt pipe.|[0010] Preferably, a pair of flexible drainage tubes are arranged on the Y-shaped shunt tube.|[0011] Preferably, the inner sides of the powder tanks are respectively provided with a plurality of clip-shaped gathering blocks.|[0012] Preferably, a plurality of magnetic drainage rods are respectively arranged on the inner sides of the plurality of crushing rollers.|[0013] The utility model provides a carbon black clearance magnetism sieve excess device. The method has the following beneficial effects: this carbon black clearance magnetism sieve excess device changes powder jar agitating unit into has magnetic agitating unit, can fully adsorb the interior ferromagnetic type impurity of likepowder carbon black, when shutting down at every turn, draws empty powder jar bottom powder, closes electromagnetic means, and the adsorbate of magnetism type drops, clears up ferromagnetic substance from the clearance mouth in order to reach the purpose that reduces washing sieve excess and improve carbon black purity.|DRAWINGS DESCRIPTION|[0014] Fig. 1 is a schematic front sectional view of a device for cleaning magnetic screen residue by carbon black of the present invention.|[0015] Fig. 2 is a schematic side view and sectional view of the device for cleaning magnetic screen residue by carbon black of the present invention.|[0016] Fig. 3 is an enlarged view of a portion "a" in fig. 1.|[0017] In the figure: 1. a powder tank; 2. a stirring shaft tube; 3. a crushing roller; 4. crushing the blocks; 5. a crushing sprocket; 6. a pulverizing driver; 7. crushing chains; 8. an electromagnet rod; 9. an inner bearing block; 10. an outer bearing block; 11. a sidewall support frame; 12. a Y-shaped shunt tube; 13. a shunt shaft; 14. a flow distribution plate; 15. a bidirectional electromagnet bar; 16. a magnet bar; 17. a concave bearing block; 18. a rotating shaft; 19. a rotating wheel; 20. a folding shutter.|INVENTION MODE|Detailed Description|[0018] The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.|[0019] Example 1|[0020] As shown in fig. 1-3, a pulverized metal collecting structure is installed inside the powder tank 1, and a flow dividing structure is installed at the bottom end of the powder tank 1;|[0021] specifically, the crushed metal collecting structure comprises: the crushing device comprises a plurality of stirring shaft tubes 2, a plurality of crushing rollers 3, a plurality of crushing blocks 4, a plurality of crushing chain wheels 5, a pair of crushing driving machines 6, a pair of crushing chains 7, a plurality of electromagnet rods 8, a plurality of inner bearing blocks 9, a plurality of outer bearing blocks 10 and a side wall support frame 11;|[0022] specifically, the lateral wall support frame 11 install in on the lateral wall of powder jar 1, a plurality of stirring central siphon 2 install in through a plurality of outer bearing piece 10 respectively in lateral wall support frame 11 and on the powder jar 1, a plurality of crushing roller 3 installs respectively in a plurality of on the stirring central siphon 2, a plurality of crushing piece 4 installs respectively in a plurality of crushing roller 3 and the inboard of powder jar 1, a plurality of electromagnet pole 8 installs respectively in a plurality of through a plurality of inner bearing piece 9 the inboard of stirring central siphon 2, it is a pair of smash driving machine 6 install in on the powder jar 1, a plurality of smash sprocket 5 install respectively in a plurality of stirring central siphon 2 and a pair of on the drive end of smash driving machine 6, it is a pair of smash chain 7 suit in a plurality of smash on the sprocket 5.|[0023] In the above, by pouring the raw material into the powder container 1 and operating the pair of pulverizing drivers 6, the pulverizing sprockets 5 on the driving ends of the pair of pulverizing drivers 6 are rotated, the crushing chain wheels 7 are respectively driven by a pair of crushing chain wheels 5, a plurality of crushing chain wheels 5 are respectively driven by a pair of crushing chain wheels 7 to rotate, the stirring shaft tubes 2 on the crushing chain wheels 5 are respectively driven by the crushing chain wheels, the crushing rollers 3 on the stirring shaft tubes 2 are respectively driven by the stirring shaft tubes 2, meanwhile, a plurality of electromagnet rods 8 in a plurality of stirring shaft tubes 2 magnetize a plurality of stirring shaft tubes 2 and the crushing rollers 3 on the stirring shaft tubes, so that a plurality of crushing rollers 3 and a plurality of crushing blocks 4 on the crushing rollers, the carbon black is crushed by a plurality of crushing blocks 4 which relatively rotate, and the iron metal component in the crushed carbon black is magnetically adsorbed.|[0024] Example 2|[0025] As shown in fig. 1-2, the shunting structure comprises: the device comprises a Y-shaped shunt pipe 12, a shunt shaft 13, a shunt plate 14, a pair of bidirectional electromagnet bars 15, magnet bars 16, a plurality of concave bearing blocks 17, a plurality of rotating shafts 18, a plurality of rotating wheels 19 and two pairs of folding shielding plates 20;|[0026] specifically, the Y-shaped shunt tube 12 is installed at the bottom end of the powder tank 1, the shunt shaft 13 is inserted into the inner side of the Y-shaped shunt tube 12, the splitter plate 14 is mounted on the splitter shaft 13, a splitter driving right-angle opening is formed on the Y-shaped splitter 12, a pair of the bidirectional electromagnet bars 15 are respectively mounted on the pair of the splitter driving right-angle openings, the magnet strips 16 are mounted on the splitter plate 14, the concave bearing blocks 17 are mounted on two sides of the splitter plate 14, the rotating shafts 18 are mounted on the concave bearing blocks 17, the rotating wheels 19 are mounted on the rotating shafts 18, the two pairs of folding shielding plates 20 are mounted on two sides of the splitter plate 14, and the two pairs of folding shielding plates 20 are connected to the inner side of the powder tank 1.|[0027] It should be noted that, in the above description, the pulverized and sieved carbon black falls into the Y-shaped shunt tube 12, and the magnet bars 16 on the shunt plate 14 are attracted to one side of the pair of shunt drive right-angle openings by one of the pair of bidirectional electromagnet bars 15 operating in the forward direction and the other one operating in the reverse direction, and repelling and adsorbing, so that the shunt plate 14 rotates along the shunt shaft 13, so that carbon black powder and ferrous metal powder are separated from each other, the shunt plate 14 and the Y-shaped shunt tube 12 are side-sealed by the two pairs of folding shielding plates 20, and the shunt plate 14 can stably rotate in the Y-shaped shunt tube 12 by the cooperation of the plurality of rotating shafts 18 on the plurality of concave bearing blocks 17 and the rotating wheels 19 thereon.|[0028] Preferably, a drainage valve is arranged at the joint of the powder tank 1 and the Y-shaped shunt pipe 12.|[0029] Preferably, a pair of flexible drainage tubes are disposed on the Y-shaped shunt 12.|[0030] Preferably, a plurality of square-shaped gathering blocks are respectively arranged on the inner sides of the powder tanks 1.|[0031] Preferably, a plurality of magnetic drainage rods are respectively arranged on the inner sides of the plurality of crushing rollers 3.|[0032] It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation. The use of the phrase "comprising one of the elements does not exclude the presence of other like elements in the process, method, article, or apparatus that comprises the element.|[0033] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. Family Number|(101804733)|101804733|Abstract|(CN217431790U U)|The utility model discloses a carbon black cleaning magnetic residue screening device which comprises a powder tank , a smashed metal collecting structure is installed on the inner side of the powder tank , and a flow dividing structure is installed at the bottom end of the powder tank . The crushed metal collecting structure comprises a plurality of stirring shaft pipes , a plurality of crushing rollers , a plurality of crushing blocks , a plurality of crushing chain wheels , a pair of crushing drivers , a pair of crushing chains , a plurality of electromagnetic iron rods , a plurality of inner bearing blocks , a plurality of outer bearing blocks and a side wall supporting frame . The utility model relates to the technical field of carbon black iron removal , a powder tank stirring device is changed into a magnetic stirring device , iron impurities in powdery carbon black can be fully adsorbed , when the machine is shut down each time , powder at the bottom of a powder tank is empty , an electromagnetic device is closed , and iron adsorbable magnetic substances fall off . And magnetic substances are cleaned from the cleaning port to achieve the purposes of reducing washing screen residues and improving the purity of the carbon black . |IPC codes|(CN217431790U U)|B01F - 033/453 |B01F - 033/83 | Basic materials chemistry|Chemical engineering B01F-033/453|B01F-033/83|B02C-004/02|B02C-023/02|B03C-001/02|C09C-001/48 B01F-033/453|B01F-033/83|B02C-004/02|B02C-023/02|B03C-001/02|C09C-001/48 GRANTED (CN217431790)|GRANTED ALIVE (CN217431790)|ALIVE (CN217431790)|LEGAL DETAILS FOR CN217431790|Actual or expected expiration date=2031-11-30|Legal state=ALIVE|Status=GRANTED|Event publication date=2021-11-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202122978429|Application date=2021-11-30|Standardized application number=2021CN-U2978429|Event publication date=2022-09-16|Event code=CN/U|Event indicator=Pos|Event group=Event indicating In Force|Registered Utility Model|Publication country=CN|Publication number=CN217431790|Publication stage code=U|Publication date=2022-09-16|Standardized publication number=CN217431790U|Event publication date=2022-09-16|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN217431790)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=jf59U3ybGzboaaWR7d/6XqqLeopS8oZMbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000064699695&ekey=2087&xpn=CN217431790U&kind=U https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=U4hy1t37oT1QZMSRYtC417msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN217431790)|CN (CN217431790)|NAME=HANCHENG HEIMAO CARTON BLACK CO., LTD. , COUNTRY=CN (CN217431790)|NAME=HUANG DEYUE;BEIJING RAINBOW XINGYUAN INTELLECTUAL PROPERTY LAW FIRM , REG=11297 (CN217431790)|NAME=MA LIPENG|NAME=CHEN ZHIFENG|NAME=FENG YANLONG|NAME=LI YONGHONG|NAME=SHI XIANGPENG 0 1 Titre: (CN217431790)|Magnetic residue screening device for cleaning carbon black Résumé: (CN217431790)|The utility model discloses a carbon black cleaning magnetic residue screening device which comprises a powder tank, a smashed metal collecting structure is installed on the inner side of the powder tank, and a flow dividing structure is installed at the bottom end of the powder tank. The crushed metal collecting structure comprises a plurality of stirring shaft pipes, a plurality of crushing rollers, a plurality of crushing blocks, a plurality of crushing chain wheels, a pair of crushing drivers, a pair of crushing chains, a plurality of electromagnetic iron rods, a plurality of inner bearing blocks, a plurality of outer bearing blocks and a side wall supporting frame. The utility model relates to the technical field of carbon black iron removal, a powder tank stirring device is changed into a magnetic stirring device, iron impurities in powdery carbon black can be fully adsorbed, when the machine is shut down each time, powder at the bottom of a powder tank is empty, an electromagnetic device is closed, and iron adsorbable magnetic substances fall off. And magnetic substances are cleaned from the cleaning port to achieve the purposes of reducing washing screen residues and improving the purity of the carbon black. 111 Abstract gpt-4o-mini no The article focuses on a device for cleaning carbon black and removing iron impurities, which does not relate to accelerated weathering or CO₂ capture.
112 CN202510619977 CN202510619977 CN120589691 115894920 CN120589691 A 2025-09-05 [CN120589691] 2025-05-14 2025-05-14 2025-09-05 (CN120589691)|2045-05-14 (CN120589691)|Method for preparing high-quality sulfur through low-quality sulfur paste hydrothermal carbon sequestration upgrading (CN120589691)|According to the technical scheme, the method comprises the following steps that firstly, the low-quality sulfur paste is crushed and screened, and turbid liquid with a certain concentration is prepared from the low-quality sulfur paste and a solvent according to the mass ratio; 2, transferring the turbid liquid into a reaction kettle, heating to a reaction temperature, and carrying out a hydrothermal reaction to obtain a black solid; 3, the black solid is subjected to solid-liquid separation through a liquefying system, insoluble substances such as fixed carbon are removed through a filtering system, and high-quality sulfur is obtained through a condensing system; the method is wide in application range, can be used for purifying low-quality sulfur with high oil content, solid content and inorganic salt content, is simple in treatment process, greatly reduces the treatment cost, adopts water and low-quality sulfur paste as main raw materials, is low in site selection requirement and high in flexibility, mainly adopts heating and cooling as main means, is short in flow, is simple and convenient to operate, and is suitable for industrial production. And implementation and control in actual operation are facilitated, and the method is an effective way for resource utilization of low-quality sulfur. XIN JIANG UNIVERSITY (CN120589691)|XIN JIANG UNIVERSITY ([CN]) HUANG HE|LIU NA|WANG XUEYING|FENG JUN|WU YULONG|HUANG XUELI (CN120589691)|HUANG HE|LIU NA|WANG XUEYING|FENG JUN|WU YULONG|HUANG XUELI (CN120589691)|WANG XU;BEIJING CHONGZHI INTELLECTUAL PROPERTY AGENT CO., LTD|Reg. Nb: 11605 (CN120589691)|In summary, the invention has the following advantages:|However, oil drops are small in the desulfurization process, oil in the low-quality sulfur paste is uniformly distributed and difficult to remove, in the low-quality sulfur paste sulfur melting and purifying process, the oil can be mixed with molten sulfur and difficult to separate, in the gasification and purifying process, the oil and the sulfur are gasified at the same time, so that the gasification and separation difficulty is doubled, and in the extraction and purifying process, the oil can enter an extracting agent, so that the extracting agent is foamed and deteriorated.| (CN120589691)|1. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading is characterized by comprising the following steps of: crushing and screening low-quality sulfur paste, preparing suspension with a certain concentration with a solvent according to a mass ratio, adding an additive with a certain proportion, and stirring for a certain time; transferring the suspension obtained in the first step into a reaction kettle, raising the reaction temperature to perform hydrothermal reaction, and obtaining black solid through hot filtration; and thirdly, solid-liquid separation of black solids is realized through a liquefying system, insoluble matters such as fixed carbon and the like are removed through a filtering system, and high-quality sulfur is obtained through a condensing system. | (CN120589691)|Aiming at the defects of the prior art, the invention provides a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon, which solves the problems in the prior art.The technical aim of the invention is realized by the following technical scheme:|The invention discloses a method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon, which comprises the following steps of crushing and screening the low-quality sulfur paste, preparing a suspension with a certain concentration with a solvent according to a mass ratio, transferring the suspension into a reaction kettle, raising the reaction temperature to perform hydrothermal reaction to obtain black solid, and carrying out solid-liquid separation on the black solid through a liquefying system, removing insoluble substances such as fixed carbon and the like through a filtering system and obtaining the high-quality sulfur through a condensing system.|The invention relates to the technical field of sulfur preparation, in particular to a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon.| (CN120589691)|LOW QUALITY SULFUR PASTE(100,25)|HIGH QUALITY SULFUR(100,19)|THERMOSETTING CARBON(100,14)|THERMOSETTING CARBON UPGRADING(69,1)|INSOLUBLE SUBSTANCE(50,1)|PASTE SULFUR MELTING(50,1)|LIQUEFACTION(47,12)|SULFUR UNEVEN CRYSTALIZATION(46,1)|REACTION KETTLE(41,7)|MOLTEN SULFUR(39,1)|CONDENSATION(37,9)|GASIFICATION(34,4)|CRUSHING(32,4)|MACROMOLECULAR SURFACTANT(32,3)|INSOLUBLE MATTER(31,10)|SEPARATION DIFFICULTY(31,1)|HYDROTHERMAL REACTION(27,6)|SUSPENSION SOLVENT(27,4)|HOT FILTRATION(27,3)|ADDITIVE(26,9)|SOLID BLACK(25,13)|REACTION TEMPERATURE(23,7)|EXTRACTING AGENT(23,2)|OIL DROP(23,1)|SULFUR MELTING KETTLE(22,3)|IMPURITY CONTENT(20,3)|DESULFURIZATION(20,1)|HYDROTHERMAL REACTION REACTOR(19,3)|SULFUR KETTLE WATER(19,3)|SULFUR(18,6)|FILTER CLOTH(17,3)|SCREENING(17,3)|SULFUR PREPARATION(16,1)|FILTERED LIQUID SULFUR(15,4)|CLOSURE REACTION KETTLE(15,3)|POLYVINYLPYRROLIDONE(15,3)|SOLID LIQUID SEPARATION(14,7)|RMP(14,6)|FILTER SCREEN(14,3)|HYDROTHERMAL REACTION STIRRING RATE(14,2)|RAPID COOLING(13,3)|MASS RATIO(12,7)|RAW GAS(11,3)|COOLING RATE(10,3)|SULFUR PRODUCT MEET(10,2)|STIRRING FUNCTION(9,3)|POST REACTION FILTRATION TEMPERATURE(9,1)|SULFUR NONUNIFORM CRYSTALIZATION(9,1)|SULFUR PASTE XRD SPECTRUM(9,1)|UNEVEN SULFUR CRYSTALIZATION(8,1)|FIXED CARBON(7,11)|FILTERING MEDIUM(7,2)|INSOLUBLE IMPURITY(7,2)|QUALITY SULFUR PASTE(7,2)|MASS CONCENTRATION(6,3)|HYDROTHERMAL CONDITION(6,2)|FILTERING TEMPERATURE(5,4)|CONDENSED HIGH QUALITY SULFUR(5,3)|QUALITY STANDARD(5,3)|SOLID SULFUR(5,3)|SOLUBLE MATTER(5,3)|UNIFORM SUSPENSION(5,3)|DANGEROUS WASTE(5,1)|HYDROTHERMAL TREATMENT(5,1)|STIRRING TIME(4,4)|BLACK SOLID SUSPENSION(4,2)|INORGANIC SALT(4,2)|SOLUBILITY(4,2)| (CN120589691)|1. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading is characterized by comprising the following steps of:| crushing and screening low-quality sulfur paste, preparing suspension with a certain concentration with a solvent according to a mass ratio, adding an additive with a certain proportion, and stirring for a certain time; | transferring the suspension obtained in the first step into a reaction kettle, raising the reaction temperature to perform hydrothermal reaction, and obtaining black solid through hot filtration; | and thirdly, solid-liquid separation of black solids is realized through a liquefying system, insoluble matters such as fixed carbon and the like are removed through a filtering system, and high-quality sulfur is obtained through a condensing system. |2. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading as claimed in claim 1, wherein the low-quality sulfur paste in the first step is high-oil-content sulfur paste generated in the process of removing H 2 S from raw gas by using a direct oxidation method.|3. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading as claimed in claim 1, wherein in the first step, the suspension solvent is water and/or sulfur melting kettle water, preferably the solvent is sulfur kettle water, wherein the concentration of the sulfur paste in the suspension solvent is 10-80% (mass concentration), preferably 50% (mass ratio), and the additive in the suspension is a macromolecular surfactant, preferably the additive is polyvinylpyrrolidone, the concentration is 0-5%, preferably the concentration is 0-0.05%.|4. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading according to claim 1, wherein in the first step, the stirring speed of the suspension is 0-2000 rmp, preferably 600rmp, and the stirring time is 0-60 minutes, preferably 30 minutes.|5. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading according to claim 1, wherein the hydrothermal reaction reactor in the second step is a closed reaction kettle with a stirring function, the stirring rate of the hydrothermal reaction is 0-1000 rmp, the preferable stirring rate is 400rmp, the temperature is 40-300 ℃, the preferable reaction temperature is 60-180 ℃, the time is 0-300 minutes, the preferable reaction time is 30 minutes, the post-reaction filtration temperature is 30-100 ℃, and the preferable filtration temperature is 60 ℃.|6. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading as claimed in claim 1, wherein in the third step, black solid suspension is introduced into a liquefying system, sulfur in the black solid is melted by heating to form liquid sulfur, preferably at 110-150 ℃, the sulfur is melted but not decomposed, after passing through the liquefying system, the suspension is subjected to solid-liquid separation by a filtering system, and fixed carbon and other insoluble matters are removed by using a proper filtering medium (such as a filter cloth or a filter screen with a preferable aperture of 1-10 microns), so that the filtered liquid sulfur is as pure as possible and has the lowest impurity content.|7. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading as claimed in claim 1, wherein in the third step, filtered liquid sulfur is introduced into a condensing system, the liquid sulfur is condensed into solid sulfur, the cooling rate is controlled to be 5-10 ℃ per minute, uneven crystallization of sulfur caused by rapid cooling is avoided, and the final condensing temperature is preferably controlled to be 30-50 ℃ to ensure complete solidification of sulfur.|8. The method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading as claimed in claim 1, wherein the condensed high-quality sulfur is finally collected in the third step, and then necessary detection is carried out to ensure that the sulfur product meets the quality standard. (CN120589691)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of sulfur preparation, in particular to a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon.|BACKGROUND ART|[0002] Coal contains a large amount of sulfur elements, which are converted into hydrogen sulfide during gasification and coking. At present, a wet oxidation-reduction method is mostly adopted to convert hydrogen sulfide into sulfur, but because crude gas carries oil, dust and other impurities, part of the oil and dust enter a sulfur product to reduce the quality of the sulfur, sulfur produced by a desulfurization device is oil-dust-containing sulfur paste and cannot be utilized, and most of the sulfur paste is treated as dangerous waste, so that the utilization rate of low-quality sulfur is improved, and most enterprises adopt matched sulfur paste refining projects to solve the problem of short plate operation of the device.|[0003] Currently, common sulfur paste purification processes include a sulfur melting method, a gasification method and an extraction method, wherein the sulfur melting method is most widely applied. However, oil drops are small in the desulfurization process, oil in the low-quality sulfur paste is uniformly distributed and difficult to remove, in the low-quality sulfur paste sulfur melting and purifying process, the oil can be mixed with molten sulfur and difficult to separate, in the gasification and purifying process, the oil and the sulfur are gasified at the same time, so that the gasification and separation difficulty is doubled, and in the extraction and purifying process, the oil can enter an extracting agent, so that the extracting agent is foamed and deteriorated. Therefore, the oil in the low quality sulfur paste is a key factor that restricts the efficient purification of the low quality sulfur paste. In order to solve the problems, we propose a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon.|DISCLOSURE|Disclosure of Invention|[0004] Aiming at the defects of the prior art, the invention provides a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon, which solves the problems in the prior art.|[0005] The technical aim of the invention is realized by the following technical scheme:|[0006] a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon comprises the following steps: |[0007] crushing and screening low-quality sulfur paste, preparing suspension with a certain concentration with a solvent according to a mass ratio, adding an additive with a certain proportion, and stirring for a certain time; |[0008] transferring the suspension obtained in the first step into a reaction kettle, raising the reaction temperature to perform hydrothermal reaction, and obtaining black solid through hot filtration; |[0009] and thirdly, solid-liquid separation of black solids is realized through a liquefying system, insoluble matters such as fixed carbon and the like are removed through a filtering system, and high-quality sulfur is obtained through a condensing system. |[0010] Preferably, the low-quality sulfur paste in the first step refers to high-oil-content sulfur paste generated in the process of removing H 2 S from raw gas by using a direct oxidation method.|[0011] Preferably, the suspension solvent in the first step is water and/or sulfur melting kettle water, preferably the solvent is sulfur kettle water, wherein the concentration of sulfur paste in the suspension solvent is 10-80% (mass concentration), preferably 50% (mass ratio), and the additive in the suspension is macromolecular surfactant, preferably the additive is polyvinylpyrrolidone, and the concentration is 0-5%, preferably 0-0.05%.|[0012] Preferably, in the first step, the stirring speed of the suspension is 0-2000 rmp, preferably 600rmp, and the stirring time is 0-60 minutes, preferably 30 minutes.|[0013] Preferably, the hydrothermal reaction reactor in the second step is a closed reaction kettle with a stirring function, the stirring rate of the hydrothermal reaction is 0-1000 rmp, the preferable rate is 400rmp, the temperature is 40-300 ℃, the preferable reaction temperature is 60-180 ℃, the time is 0-300 minutes, the preferable reaction time is 30 minutes, the filtering temperature after the reaction is 30-100 ℃, and the preferable filtering temperature is 60 ℃.|[0014] Preferably, in the third step, the black solid suspension is introduced into a liquefaction system, sulfur in the black solid is melted by heating to form liquid sulfur, preferably at 110-150 ℃, the sulfur is melted but not decomposed, after passing through the liquefaction system, the suspension is subjected to solid-liquid separation by a filtering system, and fixed carbon and other insoluble matters are removed by using a proper filtering medium (such as a filter cloth or a filter screen with a preferable aperture of 1-10 microns), so that the filtered liquid sulfur is as pure as possible and has the lowest impurity content.|[0015] Preferably, in the third step, the filtered liquid sulfur is introduced into a condensing system, the liquid sulfur is condensed into solid sulfur, the cooling rate is controlled to be 5-10 ℃ per minute, uneven sulfur crystallization caused by rapid cooling is avoided, the final condensing temperature is preferably controlled to be 30-50 ℃, and complete solidification of the sulfur is ensured.|[0016] Preferably, the condensed high-quality sulfur is finally collected in the third step, and then necessary detection is carried out to ensure that the sulfur product meets the quality standard.|[0017] In summary, the invention has the following advantages:|[0018] According to the method, the soluble parts such as inorganic salt and the like are dissolved into water under the hydrothermal condition, the oil in the low-quality sulfur paste is converted into high-crystallinity fixed carbon through the hydrothermal method, so that the solubility and boiling point of the oil are changed, soluble matters and insoluble matters in the sulfur paste are separated through filtration, sulfur in raw materials is liquefied through a liquefying system, and is separated from the fixed carbon and the insoluble matters, insoluble impurities in liquid sulfur are removed through the filtration system, and finally the high-quality sulfur is obtained through a condensing system. |DRAWINGS DESCRIPTION|[0019] FIG. 1 is a schematic diagram of the process flow structure of the method of the present invention;|[0020] fig. 2 is an XRD spectrum of the sulfur paste before and after the hydrothermal treatment of the present invention. |INVENTION MODE|Detailed Description|[0021] In order to make the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention, and it is apparent that the described embodiments are some, but not all, embodiments of the present invention, and all other embodiments obtained by persons of ordinary skill in the art without inventive labor based on the described embodiments of the present invention are included in the scope of protection of the present invention.|[0022] The following examples are illustrative of the present invention but are not intended to limit the scope of the invention. The conditions in the examples can be further adjusted according to specific conditions, and simple modifications of the method of the invention under the premise of the conception of the invention are all within the scope of the invention as claimed.|[0023] Referring to fig. 1-2, a method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading comprises the following steps:|[0024] crushing and screening low-quality sulfur paste, preparing suspension with a certain concentration with a solvent according to a mass ratio, adding an additive with a certain proportion, and stirring for a certain time; |[0025] transferring the suspension obtained in the first step into a reaction kettle, raising the reaction temperature to perform hydrothermal reaction, and obtaining black solid through hot filtration; |[0026] and thirdly, solid-liquid separation of black solids is realized through a liquefying system, insoluble matters such as fixed carbon and the like are removed through a filtering system, and high-quality sulfur is obtained through a condensing system. |[0027] Referring to fig. 1-2, the low-quality sulfur paste in the first step refers to high-oil-content sulfur paste generated in the process of removing H 2 S from raw gas by a direct oxidation method, the suspension solvent in the first step is water and/or sulfur melting kettle water, preferably the solvent is sulfur kettle water, wherein the concentration of the sulfur paste in the suspension solvent is 10-80% (mass concentration), preferably the concentration is 50% (mass ratio), and the additive in the suspension is a macromolecular surfactant, preferably the additive is polyvinylpyrrolidone, the concentration is 0-5%, preferably the concentration is 0-0.05%.|[0028] Referring to fig. 1-2, in the first step, the stirring speed of the suspension is 0-2000 rmp, the preferable speed is 600rmp, the stirring time is 0-60 minutes, the preferable stirring time is 30 minutes, the hydrothermal reaction reactor in the second step is a closed reaction kettle with a stirring function, the hydrothermal reaction stirring speed is 0-1000 rmp, the preferable speed is 400rmp, the temperature is 40-300 ℃, the preferable reaction temperature is 60-180 ℃, the time is 0-300 minutes, the preferable reaction time is 30 minutes, the filtering temperature after the reaction is 30-100 ℃, and the preferable filtering temperature is 60 ℃.|[0029] Referring to fig. 1-2, in the third step, the black solid suspension is introduced into a liquefaction system, sulfur in the black solid is melted by heating to form liquid sulfur, preferably at 110-150 ℃, the sulfur is melted but not decomposed, after passing through the liquefaction system, the suspension is subjected to solid-liquid separation by a filtration system, and fixed carbon and other insoluble matters are removed by using a proper filtration medium (such as a filter cloth or a filter screen with a preferable aperture of 1-10 microns), so that the filtered liquid sulfur is as pure as possible and has the lowest impurity content.|[0030] Referring to fig. 1-2, in the third step, filtered liquid sulfur is introduced into a condensing system, the liquid sulfur is condensed into solid sulfur, the cooling rate is controlled to be 5-10 ℃ per minute, nonuniform crystallization of sulfur caused by rapid cooling is avoided, the final condensing temperature is preferably controlled to be 30-50 ℃, complete solidification of the sulfur is ensured, the condensed high-quality sulfur is finally collected in the third step, necessary detection is carried out, and the sulfur product is ensured to meet quality standards.|[0031] Example 1|[0032] 30G of sulfur paste which is sieved by a 40-mesh sieve is added into 100g of tap water, stirring is carried out for 20 minutes at 1000rmp to obtain uniform suspension, the obtained solution is transferred into a 200ml high-pressure reaction kettle, the temperature is raised to 180 ℃, the reaction is carried out for 3 hours at the stirring rate of 600rmp, the temperature is reduced to 80 ℃, the black solid is obtained by filtering while the solution is hot, the black solid is heated to 140 ℃ to obtain liquid, and the yellow high-quality sulfur is obtained by filtering and cooling.|[0033] Example 2|[0034] 30G of sulfur paste which is sieved by a 40-mesh sieve and 0.3g of sulfur paste are added into 100g of tap water, stirring is carried out for 20 minutes at 1000rmp to obtain uniform suspension, the obtained solution is transferred into a 200ml high-pressure reaction kettle, the temperature is increased to 180 ℃, the reaction is carried out for 0.5 hour at the stirring speed of 600rmp, black solid is obtained by filtering while the solution is hot, liquid is obtained by heating the black solid to 140 ℃, and yellow high-quality sulfur is obtained by filtering and cooling.|[0035] Example 3|[0036] 30G of sulfur paste passing through a 40-mesh sieve and 0.3g of PVP are added into 100g of tap water, stirred at 1000rmp for 20 minutes to obtain uniform suspension, the obtained solution is transferred into a 200ml high-pressure reaction kettle, the temperature is raised to 60 ℃, the reaction is carried out for 10 hours under the stirring speed of 600rmp, black solid is obtained by filtering while the solution is hot, the black solid is heated to 140 ℃ to obtain liquid, and yellow high-quality sulfur is obtained by filtering and cooling.|[0037] Working principle: referring to fig. 1-2, the method is characterized in that soluble parts such as inorganic salt and the like are dissolved into water under hydrothermal conditions, oil in low-quality sulfur paste is converted into high-crystallinity fixed carbon by a hydrothermal method, so that the solubility and boiling point of the oil are changed, soluble matters and insoluble matters in the sulfur paste are separated by filtration, sulfur in raw materials is liquefied by a liquefying system, the soluble matters and the fixed carbon are separated from the insoluble matters, insoluble impurities in liquid sulfur are removed by a filtering system, and finally high-quality sulfur is obtained by a condensing system.|[0038] Although embodiments of the present invention have been shown and described, it will be understood by those of ordinary skill in the art that unless otherwise defined, technical or scientific terms used herein should be used in the ordinary sense of the present invention, and the use of the terms "comprising" or "including" or the like herein should be taken in a generic sense, to the effect that elements or items appearing before the term are covered by the terms or items listed after the term and their equivalents, without excluding other elements or items, and the terms "connected" or the like should not be limited to physical or mechanical connections, but may also include electrical connections, whether direct or indirect, "upper", "lower", "left", "right", etc. are merely intended to indicate relative positional relationships that may also be correspondingly altered when the absolute position of the subject matter being described is altered.|[0039] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. (CN120589691)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of sulfur preparation, in particular to a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon.|BACKGROUND ART|[0002] Coal contains a large amount of sulfur elements, which are converted into hydrogen sulfide during gasification and coking. At present, a wet oxidation-reduction method is mostly adopted to convert hydrogen sulfide into sulfur, but because crude gas carries oil, dust and other impurities, part of the oil and dust enter a sulfur product to reduce the quality of the sulfur, sulfur produced by a desulfurization device is oil-dust-containing sulfur paste and cannot be utilized, and most of the sulfur paste is treated as dangerous waste, so that the utilization rate of low-quality sulfur is improved, and most enterprises adopt matched sulfur paste refining projects to solve the problem of short plate operation of the device.|[0003] Currently, common sulfur paste purification processes include a sulfur melting method, a gasification method and an extraction method, wherein the sulfur melting method is most widely applied. However, oil drops are small in the desulfurization process, oil in the low-quality sulfur paste is uniformly distributed and difficult to remove, in the low-quality sulfur paste sulfur melting and purifying process, the oil can be mixed with molten sulfur and difficult to separate, in the gasification and purifying process, the oil and the sulfur are gasified at the same time, so that the gasification and separation difficulty is doubled, and in the extraction and purifying process, the oil can enter an extracting agent, so that the extracting agent is foamed and deteriorated. Therefore, the oil in the low quality sulfur paste is a key factor that restricts the efficient purification of the low quality sulfur paste. In order to solve the problems, we propose a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon.|DISCLOSURE|Disclosure of Invention|[0004] Aiming at the defects of the prior art, the invention provides a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon, which solves the problems in the prior art.|[0005] The technical aim of the invention is realized by the following technical scheme:|[0006] a method for preparing high-quality sulfur by upgrading low-quality sulfur paste water thermosetting carbon comprises the following steps: |[0007] crushing and screening low-quality sulfur paste, preparing suspension with a certain concentration with a solvent according to a mass ratio, adding an additive with a certain proportion, and stirring for a certain time; |[0008] transferring the suspension obtained in the first step into a reaction kettle, raising the reaction temperature to perform hydrothermal reaction, and obtaining black solid through hot filtration; |[0009] and thirdly, solid-liquid separation of black solids is realized through a liquefying system, insoluble matters such as fixed carbon and the like are removed through a filtering system, and high-quality sulfur is obtained through a condensing system. |[0010] Preferably, the low-quality sulfur paste in the first step refers to high-oil-content sulfur paste generated in the process of removing H 2 S from raw gas by using a direct oxidation method.|[0011] Preferably, the suspension solvent in the first step is water and/or sulfur melting kettle water, preferably the solvent is sulfur kettle water, wherein the concentration of sulfur paste in the suspension solvent is 10-80% (mass concentration), preferably 50% (mass ratio), and the additive in the suspension is macromolecular surfactant, preferably the additive is polyvinylpyrrolidone, and the concentration is 0-5%, preferably 0-0.05%.|[0012] Preferably, in the first step, the stirring speed of the suspension is 0-2000 rmp, preferably 600rmp, and the stirring time is 0-60 minutes, preferably 30 minutes.|[0013] Preferably, the hydrothermal reaction reactor in the second step is a closed reaction kettle with a stirring function, the stirring rate of the hydrothermal reaction is 0-1000 rmp, the preferable rate is 400rmp, the temperature is 40-300 ℃, the preferable reaction temperature is 60-180 ℃, the time is 0-300 minutes, the preferable reaction time is 30 minutes, the filtering temperature after the reaction is 30-100 ℃, and the preferable filtering temperature is 60 ℃.|[0014] Preferably, in the third step, the black solid suspension is introduced into a liquefaction system, sulfur in the black solid is melted by heating to form liquid sulfur, preferably at 110-150 ℃, the sulfur is melted but not decomposed, after passing through the liquefaction system, the suspension is subjected to solid-liquid separation by a filtering system, and fixed carbon and other insoluble matters are removed by using a proper filtering medium (such as a filter cloth or a filter screen with a preferable aperture of 1-10 microns), so that the filtered liquid sulfur is as pure as possible and has the lowest impurity content.|[0015] Preferably, in the third step, the filtered liquid sulfur is introduced into a condensing system, the liquid sulfur is condensed into solid sulfur, the cooling rate is controlled to be 5-10 ℃ per minute, uneven sulfur crystallization caused by rapid cooling is avoided, the final condensing temperature is preferably controlled to be 30-50 ℃, and complete solidification of the sulfur is ensured.|[0016] Preferably, the condensed high-quality sulfur is finally collected in the third step, and then necessary detection is carried out to ensure that the sulfur product meets the quality standard.|[0017] In summary, the invention has the following advantages:|[0018] According to the method, the soluble parts such as inorganic salt and the like are dissolved into water under the hydrothermal condition, the oil in the low-quality sulfur paste is converted into high-crystallinity fixed carbon through the hydrothermal method, so that the solubility and boiling point of the oil are changed, soluble matters and insoluble matters in the sulfur paste are separated through filtration, sulfur in raw materials is liquefied through a liquefying system, and is separated from the fixed carbon and the insoluble matters, insoluble impurities in liquid sulfur are removed through the filtration system, and finally the high-quality sulfur is obtained through a condensing system. |DRAWINGS DESCRIPTION|[0019] FIG. 1 is a schematic diagram of the process flow structure of the method of the present invention;|[0020] fig. 2 is an XRD spectrum of the sulfur paste before and after the hydrothermal treatment of the present invention. |INVENTION MODE|Detailed Description|[0021] In order to make the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention, and it is apparent that the described embodiments are some, but not all, embodiments of the present invention, and all other embodiments obtained by persons of ordinary skill in the art without inventive labor based on the described embodiments of the present invention are included in the scope of protection of the present invention.|[0022] The following examples are illustrative of the present invention but are not intended to limit the scope of the invention. The conditions in the examples can be further adjusted according to specific conditions, and simple modifications of the method of the invention under the premise of the conception of the invention are all within the scope of the invention as claimed.|[0023] Referring to fig. 1-2, a method for preparing high-quality sulfur by using low-quality sulfur paste water thermosetting carbon upgrading comprises the following steps:|[0024] crushing and screening low-quality sulfur paste, preparing suspension with a certain concentration with a solvent according to a mass ratio, adding an additive with a certain proportion, and stirring for a certain time; |[0025] transferring the suspension obtained in the first step into a reaction kettle, raising the reaction temperature to perform hydrothermal reaction, and obtaining black solid through hot filtration; |[0026] and thirdly, solid-liquid separation of black solids is realized through a liquefying system, insoluble matters such as fixed carbon and the like are removed through a filtering system, and high-quality sulfur is obtained through a condensing system. |[0027] Referring to fig. 1-2, the low-quality sulfur paste in the first step refers to high-oil-content sulfur paste generated in the process of removing H 2 S from raw gas by a direct oxidation method, the suspension solvent in the first step is water and/or sulfur melting kettle water, preferably the solvent is sulfur kettle water, wherein the concentration of the sulfur paste in the suspension solvent is 10-80% (mass concentration), preferably the concentration is 50% (mass ratio), and the additive in the suspension is a macromolecular surfactant, preferably the additive is polyvinylpyrrolidone, the concentration is 0-5%, preferably the concentration is 0-0.05%.|[0028] Referring to fig. 1-2, in the first step, the stirring speed of the suspension is 0-2000 rmp, the preferable speed is 600rmp, the stirring time is 0-60 minutes, the preferable stirring time is 30 minutes, the hydrothermal reaction reactor in the second step is a closed reaction kettle with a stirring function, the hydrothermal reaction stirring speed is 0-1000 rmp, the preferable speed is 400rmp, the temperature is 40-300 ℃, the preferable reaction temperature is 60-180 ℃, the time is 0-300 minutes, the preferable reaction time is 30 minutes, the filtering temperature after the reaction is 30-100 ℃, and the preferable filtering temperature is 60 ℃.|[0029] Referring to fig. 1-2, in the third step, the black solid suspension is introduced into a liquefaction system, sulfur in the black solid is melted by heating to form liquid sulfur, preferably at 110-150 ℃, the sulfur is melted but not decomposed, after passing through the liquefaction system, the suspension is subjected to solid-liquid separation by a filtration system, and fixed carbon and other insoluble matters are removed by using a proper filtration medium (such as a filter cloth or a filter screen with a preferable aperture of 1-10 microns), so that the filtered liquid sulfur is as pure as possible and has the lowest impurity content.|[0030] Referring to fig. 1-2, in the third step, filtered liquid sulfur is introduced into a condensing system, the liquid sulfur is condensed into solid sulfur, the cooling rate is controlled to be 5-10 ℃ per minute, nonuniform crystallization of sulfur caused by rapid cooling is avoided, the final condensing temperature is preferably controlled to be 30-50 ℃, complete solidification of the sulfur is ensured, the condensed high-quality sulfur is finally collected in the third step, necessary detection is carried out, and the sulfur product is ensured to meet quality standards.|[0031] Example 1|[0032] 30G of sulfur paste which is sieved by a 40-mesh sieve is added into 100g of tap water, stirring is carried out for 20 minutes at 1000rmp to obtain uniform suspension, the obtained solution is transferred into a 200ml high-pressure reaction kettle, the temperature is raised to 180 ℃, the reaction is carried out for 3 hours at the stirring rate of 600rmp, the temperature is reduced to 80 ℃, the black solid is obtained by filtering while the solution is hot, the black solid is heated to 140 ℃ to obtain liquid, and the yellow high-quality sulfur is obtained by filtering and cooling.|[0033] Example 2|[0034] 30G of sulfur paste which is sieved by a 40-mesh sieve and 0.3g of sulfur paste are added into 100g of tap water, stirring is carried out for 20 minutes at 1000rmp to obtain uniform suspension, the obtained solution is transferred into a 200ml high-pressure reaction kettle, the temperature is increased to 180 ℃, the reaction is carried out for 0.5 hour at the stirring speed of 600rmp, black solid is obtained by filtering while the solution is hot, liquid is obtained by heating the black solid to 140 ℃, and yellow high-quality sulfur is obtained by filtering and cooling.|[0035] Example 3|[0036] 30G of sulfur paste passing through a 40-mesh sieve and 0.3g of PVP are added into 100g of tap water, stirred at 1000rmp for 20 minutes to obtain uniform suspension, the obtained solution is transferred into a 200ml high-pressure reaction kettle, the temperature is raised to 60 ℃, the reaction is carried out for 10 hours under the stirring speed of 600rmp, black solid is obtained by filtering while the solution is hot, the black solid is heated to 140 ℃ to obtain liquid, and yellow high-quality sulfur is obtained by filtering and cooling.|[0037] Working principle: referring to fig. 1-2, the method is characterized in that soluble parts such as inorganic salt and the like are dissolved into water under hydrothermal conditions, oil in low-quality sulfur paste is converted into high-crystallinity fixed carbon by a hydrothermal method, so that the solubility and boiling point of the oil are changed, soluble matters and insoluble matters in the sulfur paste are separated by filtration, sulfur in raw materials is liquefied by a liquefying system, the soluble matters and the fixed carbon are separated from the insoluble matters, insoluble impurities in liquid sulfur are removed by a filtering system, and finally high-quality sulfur is obtained by a condensing system.|[0038] Although embodiments of the present invention have been shown and described, it will be understood by those of ordinary skill in the art that unless otherwise defined, technical or scientific terms used herein should be used in the ordinary sense of the present invention, and the use of the terms "comprising" or "including" or the like herein should be taken in a generic sense, to the effect that elements or items appearing before the term are covered by the terms or items listed after the term and their equivalents, without excluding other elements or items, and the terms "connected" or the like should not be limited to physical or mechanical connections, but may also include electrical connections, whether direct or indirect, "upper", "lower", "left", "right", etc. are merely intended to indicate relative positional relationships that may also be correspondingly altered when the absolute position of the subject matter being described is altered.|[0039] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents. Family Number|(115894920)|115894920|Abstract|(CN120589691 A)|According to the technical scheme , the method comprises the following steps that firstly , the low - quality sulfur paste is crushed and screened , and turbid liquid with a certain concentration is prepared from the low - quality sulfur paste and a solvent according to the mass ratio ; 2, transferring the turbid liquid into a reaction kettle , heating to a reaction temperature , and carrying out a hydrothermal reaction to obtain a black solid ; 3, the black solid is subjected to solid - liquid separation through a liquefying system , insoluble substances such as fixed carbon are removed through a filtering system , and high - quality sulfur is obtained through a condensing system ; the method is wide in application range , can be used for purifying low - quality sulfur with high oil content , solid content and inorganic salt content , is simple in treatment process , greatly reduces the treatment cost , adopts water and low - quality sulfur paste as main raw materials , is low in site selection requirement and high in flexibility , mainly adopts heating and cooling as main means , is short in flow , is simple and convenient to operate , and is suitable for industrial production . And implementation and control in actual operation are facilitated , and the method is an effective way for resource utilization of low - quality sulfur . |CPC codes|(CN120589691 A)|C01B - 017/02/32 |IPC codes|(CN120589691 A)|C01B - 017/027 |C01B - 017/033 |Title|(CN120589691 A)|Method for preparing high - quality sulfur through low - quality sulfur paste hydrothermal carbon sequestration upgrading | Materials, metallurgy C01B-017/02/16|C01B-017/02/21|C01B-017/02/32|C01B-017/027|C01B-017/033 C01B-017/02/16|C01B-017/02/21|C01B-017/02/32|C01B-017/027|C01B-017/033 C01B-017/027|C01B-017/033 C01B-017/027|C01B-017/033 PENDING (CN120589691)|PENDING ALIVE (CN120589691)|ALIVE (CN120589691)|LEGAL DETAILS FOR CN120589691|Actual or expected expiration date=2045-05-14|Legal state=ALIVE|Status=PENDING|Event publication date=2025-05-14|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510619977|Application date=2025-05-14|Standardized application number=2025CN-0619977|Event publication date=2025-09-05|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120589691|Publication stage code=A|Publication date=2025-09-05|Standardized publication number=CN120589691|Event publication date=2025-09-05|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-09-23|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN120589691)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKdbwlzGCBttNlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000078859548&ekey=2310&xpn=CN120589691&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252Bud3bUVziCZNdbnROkuV15NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN120589691)|CN (CN120589691)|NAME=XIN JIANG UNIVERSITY , COUNTRY=CN (CN120589691)|NAME=WANG XU;BEIJING CHONGZHI INTELLECTUAL PROPERTY AGENT CO., LTD , REG=11605 (CN120589691)|CN (CN120589691)|NAME=HUANG HE, COUNTRY=CN |NAME=LIU NA|NAME=WANG XUEYING|NAME=FENG JUN|NAME=WU YULONG|NAME=HUANG XUELI 0 1 Titre: (CN120589691)|Method for preparing high-quality sulfur through low-quality sulfur paste hydrothermal carbon sequestration upgrading Résumé: (CN120589691)|According to the technical scheme, the method comprises the following steps that firstly, the low-quality sulfur paste is crushed and screened, and turbid liquid with a certain concentration is prepared from the low-quality sulfur paste and a solvent according to the mass ratio; 2, transferring the turbid liquid into a reaction kettle, heating to a reaction temperature, and carrying out a hydrothermal reaction to obtain a black solid; 3, the black solid is subjected to solid-liquid separation through a liquefying system, insoluble substances such as fixed carbon are removed through a filtering system, and high-quality sulfur is obtained through a condensing system; the method is wide in application range, can be used for purifying low-quality sulfur with high oil content, solid content and inorganic salt content, is simple in treatment process, greatly reduces the treatment cost, adopts water and low-quality sulfur paste as main raw materials, is low in site selection requirement and high in flexibility, mainly adopts heating and cooling as main means, is short in flow, is simple and convenient to operate, and is suitable for industrial production. And implementation and control in actual operation are facilitated, and the method is an effective way for resource utilization of low-quality sulfur. 114 Abstract gpt-4o-mini no The article focuses on a method for purifying low-quality sulfur and does not mention mineral weathering, CO₂ capture, or related processes.
113 CN202111157076 CN202111157076 CN113687055 97173977 CN113687055 A 2021-11-23 [CN113687055] 2021-09-30 2021-09-30 2021-11-23 (CN113687055)|2023-09-01 (CN113687055)|Method for testing performance and carbon dioxide sequestration capacity of solid waste-based foam concrete (CN113687055)|The invention discloses a method for testing the performance and carbon dioxide storage capacity of solid waste-based foam concrete. The method comprises the following steps: 1, preparing a solid waste-based foam concrete material performance and carbon dioxide storage capacity test bed; 2, injecting the same amount of foam concrete material into a left tray and a right tray for sealing; 3, introducing carbon dioxide into a left box body, and analyzing the storage amount of the foam concrete material on the carbon dioxide and the temperature evolution rule in the storage process; 4, repeating the second step and the third step, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material; and 5, testing the compressive strength of the solid waste-based foam concrete material after curing, and testing whether carbon dioxide overflows after the concrete material is crushed. The method is used for researching the strength change of the solid waste-based foam concrete in the carbon dioxide sealing process and the influence of different initial fluidity, temperature and carbon dioxide pressure on the sealing or curing of the solid waste-based foam concrete. SHANDONG UNIVERSITY OF SCIENCE & TECHNOLOGY (CN113687055)|SHANDONG UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) SUN LULU|DUAN SHOULEI|WANG GANG|WANG HAISHAN|CAO XIAOQIANG|XIN LIN (CN113687055)|SUN LULU|DUAN SHOULEI|WANG GANG|WANG HAISHAN|CAO XIAOQIANG|XIN LIN (CN113687055)|TAN XIAORONG;CHONGQING TIANCHENGHZUOYUE PATENT AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 50240 (CN113687055)|The invention has the beneficial effects that: the visual transparent box body with the partition plate is adopted, and combined with the combined action of an electronic balance with scales, a compressive strength tester, a temperature sensor, a carbon dioxide concentration monitor, a heating rod, a supporting frame and the like, the visual transparent box body is used for testing the performance of the solid waste base foam concrete material and the capability of sealing and storing carbon dioxide; the method is used for researching the strength change of the solid waste base foam concrete in the process of sealing carbon dioxide, different initial fluidity, temperature and carbon dioxide pressure, and the influence on the sealing or curing of the solid waste base foam concrete, so as to find out the optimal parameter of the carbon dioxide which is completely cured in the solid waste base foam concrete material; the method has the advantages that the method is more intuitive, reliable, convenient, strong in contrast and strong in operability, and has important guiding significance for guiding safe and scientific exploitation of coal seams by researching the curing action process of the solid waste base foam concrete on carbon dioxide, the influence of the temperature difference of different buried coal rock layers on the curing stress of the solid waste base foam concrete and the supporting effect of the cured coal rock layers on the top plate, fully utilizing the underground waste space and effectively controlling the natural ignition danger of the goaf.| (CN113687055)|1. A method for testing the performance and the carbon dioxide sequestration capacity of solid waste foam concrete is characterized by comprising the following steps: firstly, preparing a test bed for the performance of a solid waste base foam concrete material and the capability of sealing and storing carbon dioxide; the test bed for testing the performance of the solid waste base foam concrete material and the capability of sealing carbon dioxide comprises a sealed transparent box (1) and a carbon dioxide steel cylinder (2), a partition board (1a) is arranged in the sealed transparent box (1) to divide the space in the box into a left box body and a right box body, an electronic balance (3) is fixedly arranged at the bottom of the sealed transparent box (1), a left tray (3a) and a right tray (3a) of the electronic balance (3) respectively extend into the left box body and the right box body which respectively correspond to each other, scale marks are drawn at the bottom of the trays (3a), a telescopic compressive strength tester (4) is arranged above each tray (3a), a telescopic supporting frame (11) is arranged below each tray, the left box body and the right box body are respectively provided with a temperature sensor (5) and a carbon dioxide concentration monitor (6) No. 1, heating rods (9) are respectively arranged at the bottoms of the left box body and the right box body, solid waste base foam concrete material feeding ports (7) are respectively arranged on the left box body and the right box body, the carbon dioxide steel cylinder (2) is connected with the left box body through a pipeline (10), and a No. 2 carbon dioxide concentration monitor (12) and a valve (8) are arranged on the pipeline (10); secondly, injecting the same amount of foam concrete materials into left and right trays (3a) through solid waste base foam concrete material inlets (7) on left and right boxes by using the same pressure injection equipment to seal the foam concrete materials prepared from the solid waste bases, wherein scales are drawn at the bottom of each tray (3a), and the initial fluidity of the sealed materials is judged by observing the diffusion distance of the sealed materials on the trays (3 a); thirdly, leveling the electronic balance (3), opening a valve (8) on a pipeline (10), introducing a certain amount of carbon dioxide into the left box body, observing data change of the electronic balance (3), temperature change monitored by temperature sensors (5) of the left box body and the right box body and concentration change parameters monitored by a carbon dioxide concentration monitor (6) No. 1, and analyzing the sealing amount of the foam concrete material to the carbon dioxide and the temperature evolution rule in the sealing process; fourthly, repeating the second step and the third step, raising the temperature of the left box body and the right box body to the same temperature through a heating rod (9), changing the injection pressure of carbon dioxide through a valve (8) on an adjusting pipeline (10), observing the readings of the electronic balance (3), the temperature sensor (5) and the No. 1 carbon dioxide concentration monitor (6) again, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material; fifthly, after each sealing experiment is finished, the supporting frame (11) is lifted to support the tray (3a), the anti-compression experiment tester (4) is lowered to be in contact with the solid waste base foam concrete material in the tray (3a), the solidified solid waste base foam concrete material is gradually pressurized, the anti-compression strength of the solidified solid waste base foam concrete material is tested, whether carbon dioxide overflows after the concrete material is crushed or not is judged, whether the carbon dioxide is solidified by chemical reaction or physically sealed in the material is judged, and meanwhile, the influence of the carbon dioxide on the strength increment of the solid waste base foam concrete material is analyzed.| (CN113687055)|The invention aims to provide a method for testing the performance of a solid waste base foam concrete material and the capability of sealing carbon dioxide, which is used for researching the strength change of the solid waste base foam concrete in the process of sealing carbon dioxide, and the influence of different initial fluidity, temperature and carbon dioxide pressure on the sealing or curing of the solid waste base foam concrete.|The invention discloses a method for testing the performance and the carbon dioxide sealing capacity of solid waste base foam concrete, which comprises the following steps of firstly, preparing a test bed for testing the performance and the carbon dioxide sealing capacity of a solid waste base foam concrete material; secondly, injecting the same amount of foam concrete materials into the left tray and the right tray for sealing; thirdly, introducing carbon dioxide into the left box body, and analyzing the sealing amount of the foam concrete material to the carbon dioxide and the temperature evolution rule in the sealing and storing process; fourthly, repeating the second step and the third step, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material; and fifthly, testing the compressive strength of the solid waste base foam concrete material after curing and whether carbon dioxide overflows after the concrete material is crushed.|The invention relates to the technical field of solid waste base foam concrete performance test methods, and is used for testing the performance of solid waste base foam concrete materials and the capability of sealing carbon dioxide.| (CN113687055)|CARBON DIOXIDE(100,84)|SOLID WASTE(100,62)|BASE FOAM CONCRETE(100,25)|FOAM CONCRETE(100,12)|CARBON DIOXIDE SEQUESTRATION CAPACITY(100,8)|SEQUESTRATION CAPACITY(100,8)|SOLID WASTE FOAM CONCRETE(100,8)|FLUIDITY INFLUENCE(100,6)|SEALING CAPABILITY(100,6)|CARBON DIOXIDE(100,5)|SOLID WASTE TESTING PERFORMANCE(100,1)|COAL SEAM SCIENTIFIC EXPLOITATION(80,1)|MONITORING CONCENTRATION(64,11)|SEALED TRANSPARENT BOX(64,5)|GOAF NATURAL IGNITION DANGER(61,2)|VISUAL TRANSPARENT BOX(59,2)|SCIENTIFIC EXPLOITATION(58,1)|LEFT BOX(55,41)|ANTICOMPRESSION STRENGTH(55,1)|SEALING CAPACITY(51,2)|RIGHT BOX(50,37)|TRAY(50,24)|CARBON DIOXIDE CONCENTRATION MONITOR(49,11)|GUIDING SIGNIFICANCE(49,1)|COMPRESSIVE STRENGTH TESTER(44,13)|SEALING CARBON DIOXIDE(42,6)|ANTICOMPRESSION(42,1)|NATURAL IGNITION DANGER(41,2)|TEST BED(40,8)|BURIED COAL ROCK LAYER(40,1)|CARBON DIOXIDE SEALING CAPACITY(39,2)|PIPELINE(38,14)|TEMPERATURE EVOLUTION(38,4)|ADJUSTING PIPELINE(38,2)|UNDERGROUND WASTE SPACE(37,1)|HEATING ROD(36,11)|RIGHT TRAY(36,7)|CURING(36,4)|GUIDING SAFE(36,1)|CARBON DIOXIDE OVERFLOW(35,5)|COAL ROCK LAYER(35,2)|PARTITION BOARD(33,3)|SEALING EXPERIMENT(33,3)|STRENGTH INCREMENT(33,2)|CURED COAL ROCK LAYER(33,1)|ELECTRONIC BALANCE(32,17)|SEALING CARBON DIOXIDE CAPABILITY(31,3)|STEEL CYLINDER(30,7)|SOLID WASTE SOLIDIFICATION(29,6)|PARTITION PLATE(29,3)|COMPRESSIVE STRENGTH(27,14)|LEFT TRAY(27,5)|FLUIDITY(27,2)|FOAM CONCRETE MATERIAL(26,13)|OPERABILITY(25,1)|INJECTION PRESSURE(24,5)|SCALE MARK(24,3)|BASE FOAM CONCRETE MATERIAL(23,22)|CARBON DIOXIDE STEEL CYLINDER(23,7)|DATA OBSERVATION(23,2)|CONCRETE MATERIAL(22,4)|COAL SEAM(22,1)|CARBON DIOXIDE PRESSURE(20,3)|DIFFUSION(20,3)|SEALING(19,18)|ELECTRONIC BALANCE READING(18,3)|SEALING CARBON DIOXIDE(18,3)|TELESCOPIC SUPPORTING FRAME(18,3)|ACTION COMBINATION(18,1)|TESTER(17,3)|PRESSURE INJECTION EQUIPMENT(17,2)|MATERIAL FEED(16,3)|TEMPERATURE SENSOR(15,14)|SEALING MATERIAL(15,4)|ELECTRONIC BALANCE COMBINED ACTION(15,1)|CLOSED TRANSPARENT BOX(14,7)|LEFT BOX BOTTOM(13,5)|ACRYLIC PLATE(13,3)|SOLID WASTE PERFORMANCE(13,2)|SUPPORTING FRAME(12,5)|LEFT BOX TEMPERATURE(12,3)|TEMPERATURE DIFFERENCE(12,2)|CHEMICAL REACTION(12,1)|METAL TRAY(11,3)|SEALING(11,3)|PERFORMANCE TEST(11,1)|CHANGING TEMPERATURE(9,3)|MATERIAL INLET(9,3)|SEALING FLUIDITY(6,1)|UNDERGROUND WASTE(6,1)|LEFT BOX TOP(5,3)| (CN113687055)|1. A method for testing the performance and the carbon dioxide sequestration capacity of solid waste foam concrete is characterized by comprising the following steps:|firstly, preparing a test bed for the performance of a solid waste base foam concrete material and the capability of sealing and storing carbon dioxide;|the test bed for testing the performance of the solid waste base foam concrete material and the capability of sealing carbon dioxide comprises a sealed transparent box (1) and a carbon dioxide steel cylinder (2), a partition board (1a) is arranged in the sealed transparent box (1) to divide the space in the box into a left box body and a right box body, an electronic balance (3) is fixedly arranged at the bottom of the sealed transparent box (1), a left tray (3a) and a right tray (3a) of the electronic balance (3) respectively extend into the left box body and the right box body which respectively correspond to each other, scale marks are drawn at the bottom of the trays (3a), a telescopic compressive strength tester (4) is arranged above each tray (3a), a telescopic supporting frame (11) is arranged below each tray, the left box body and the right box body are respectively provided with a temperature sensor (5) and a carbon dioxide concentration monitor (6) No. 1, heating rods (9) are respectively arranged at the bottoms of the left box body and the right box body, solid waste base foam concrete material feeding ports (7) are respectively arranged on the left box body and the right box body, the carbon dioxide steel cylinder (2) is connected with the left box body through a pipeline (10), and a No. 2 carbon dioxide concentration monitor (12) and a valve (8) are arranged on the pipeline (10);|secondly, injecting the same amount of foam concrete materials into left and right trays (3a) through solid waste base foam concrete material inlets (7) on left and right boxes by using the same pressure injection equipment to seal the foam concrete materials prepared from the solid waste bases, wherein scales are drawn at the bottom of each tray (3a), and the initial fluidity of the sealed materials is judged by observing the diffusion distance of the sealed materials on the trays (3 a);|thirdly, leveling the electronic balance (3), opening a valve (8) on a pipeline (10), introducing a certain amount of carbon dioxide into the left box body, observing data change of the electronic balance (3), temperature change monitored by temperature sensors (5) of the left box body and the right box body and concentration change parameters monitored by a carbon dioxide concentration monitor (6) No. 1, and analyzing the sealing amount of the foam concrete material to the carbon dioxide and the temperature evolution rule in the sealing process;|fourthly, repeating the second step and the third step, raising the temperature of the left box body and the right box body to the same temperature through a heating rod (9), changing the injection pressure of carbon dioxide through a valve (8) on an adjusting pipeline (10), observing the readings of the electronic balance (3), the temperature sensor (5) and the No. 1 carbon dioxide concentration monitor (6) again, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material;|fifthly, after each sealing experiment is finished, the supporting frame (11) is lifted to support the tray (3a), the anti-compression experiment tester (4) is lowered to be in contact with the solid waste base foam concrete material in the tray (3a), the solidified solid waste base foam concrete material is gradually pressurized, the anti-compression strength of the solidified solid waste base foam concrete material is tested, whether carbon dioxide overflows after the concrete material is crushed or not is judged, whether the carbon dioxide is solidified by chemical reaction or physically sealed in the material is judged, and meanwhile, the influence of the carbon dioxide on the strength increment of the solid waste base foam concrete material is analyzed.|2. The method for testing the performance and the carbon dioxide sequestration capacity of the solid waste foam concrete according to claim 1, which is characterized in that: the support frame (10) is provided with a compressive strength tester (4).|3. The method for testing the performance and the carbon dioxide sequestration capacity of the solid waste foam concrete according to claim 1, which is characterized in that: the solid waste base foam concrete material feeding port (7) and the interface connected with the pipeline (10) are arranged on the side walls of the left box body and the right box body, and the temperature sensor (5) and the No. 1 carbon dioxide concentration monitor (6) are arranged on the tops of the left box body and the right box body.|4. The method for testing the performance and the carbon dioxide sequestration capacity of the solid waste foam concrete according to claim 1, which is characterized in that: the heating rods (9) are uniformly paved at the bottoms of the left box body and the right box body.|5. The method for testing the performance and the carbon dioxide sequestration capacity of the solid waste foam concrete according to claim 1, which is characterized in that: the circumference of the tray (3a) is provided with a surrounding edge, and the size of a pressure head of the compressive strength tester (4) is matched with the size of the inner space of the circumferential surrounding edge of the tray (3 a).|6. The method for testing the performance and the carbon dioxide sequestration capacity of the solid waste foam concrete according to claim 1, which is characterized in that: the closed transparent box (1) and the partition plate (1a) are both made of acrylic plates, and the tray (3a) is a metal tray. (CN113687055)|TECHNICAL FIELD|[0001] The invention relates to the technical field of solid waste base foam concrete performance test methods, and is used for testing the performance of solid waste base foam concrete materials and the capability of sealing carbon dioxide.|BACKGROUND ART|[0002] The solid waste base foam concrete mainly comprises solid waste base materials such as fly ash, carbide slag and the like. In the technical field of coal mining, the solid waste base foam concrete is used for sealing and curing carbon dioxide, so that the safety of coal mining can be ensured. However, the temperature difference of different buried depth coal rock layers is large, and the supporting effect of the top plate is different due to different sealed and solidified stresses. At present, no scientific research system and test method exists for the material performance of solid waste base foam concrete, and how to fully utilize underground waste space to carry out carbon dioxide sealing and curing and effectively manage the natural ignition danger of a goaf due to the influence of different temperatures and carbon dioxide injection pressures on the sealing and storing capacity of the foam concrete material.|DISCLOSURE|Disclosure of Invention|[0003] The invention aims to provide a method for testing the performance of a solid waste base foam concrete material and the capability of sealing carbon dioxide, which is used for researching the strength change of the solid waste base foam concrete in the process of sealing carbon dioxide, and the influence of different initial fluidity, temperature and carbon dioxide pressure on the sealing or curing of the solid waste base foam concrete.|[0004] Therefore, the technical scheme adopted by the invention is as follows: a method for testing the performance and the carbon dioxide sequestration capacity of solid waste foam concrete comprises the following steps:|[0005] firstly, preparing a test bed for the performance of a solid waste base foam concrete material and the capability of sealing and storing carbon dioxide;|[0006] the test bed for the performance and the capability of sealing and storing carbon dioxide of the solid waste base foam concrete material comprises a sealed transparent box and a carbon dioxide steel cylinder, a partition board is arranged in the sealed transparent box to divide the space in the box into a left box body and a right box body, an electronic balance is fixedly arranged at the bottom of the closed transparent box, a left tray and a right tray of the electronic balance respectively extend into the corresponding left box body and the corresponding right box body, scale marks are drawn at the bottoms of the trays, a telescopic compressive strength tester is arranged above each tray, a telescopic supporting frame is arranged below each tray, the left box body and the right box body are respectively provided with a temperature sensor and a carbon dioxide concentration monitor No. 1, heating rods are respectively arranged at the bottoms of the left box body and the right box body, solid waste base foam concrete material feeding ports are respectively arranged on the left box body and the right box body, carbon dioxide steel cylinders are connected with the left box body through pipelines, and the carbon dioxide concentration monitors No. 2 and valves are arranged on the pipelines;|[0007] secondly, injecting the same amount of foam concrete materials into left and right trays through solid waste base foam concrete material feed inlets on left and right box bodies for sealing and storing by the same pressure injection equipment, wherein scales are drawn at the bottom of each tray, and the initial fluidity of the sealing and storing material is judged by observing the diffusion distance of the sealing and storing material on the trays;|[0008] leveling an electronic balance, opening a valve on a pipeline, introducing a certain amount of carbon dioxide into the left box body, observing data change of the electronic balance, temperature change monitored by temperature sensors of the left box body and the right box body and concentration change parameters monitored by a carbon dioxide concentration monitor No. 1, and analyzing the sealing amount of the foam concrete material to the carbon dioxide and the temperature evolution rule in the sealing process;|[0009] fourthly, repeating the second step and the third step, raising the temperature of the left box body and the right box body to the same temperature through the heating rod, changing the injection pressure of the carbon dioxide through adjusting a valve on a pipeline, observing the readings of the electronic balance, the temperature sensor and the No. 1 carbon dioxide concentration monitor again, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material;|[0010] and fifthly, after the sealing experiment is performed each time, lifting the supporting frame to support the tray, lowering the compression resistance experiment tester to be in contact with the solid waste base foam concrete material in the tray, gradually pressurizing the solidified solid waste base foam concrete material, testing the compression resistance strength of the solidified solid waste base foam concrete material, and judging whether carbon dioxide overflows after the concrete material is crushed, so as to judge whether the carbon dioxide is subjected to chemical reaction solidification or is physically sealed in the material, and simultaneously analyzing the influence of the carbon dioxide on the strength increment of the solid waste base foam concrete material.|[0011] Preferably, the support frame is provided with a compressive strength tester.|[0012] Preferably, the solid waste base foam concrete material inlet and the interface connected with the pipeline are both arranged on the side walls of the left box body and the right box body.|[0013] More preferably, the heating rods are uniformly laid at the bottoms of the left box body and the right box body, and the temperature sensors and the No. 1 carbon dioxide concentration monitors are arranged at the tops of the left box body and the right box body.|[0014] Further preferably, the circumference of the tray is provided with a surrounding edge, and the size of the pressure head of the compressive strength tester is matched with the size of the inner space of the circumferential surrounding edge of the tray.|[0015] Preferably, the closed transparent box and the partition plate are both made of acrylic plates, and the tray is a metal tray.|[0016] The invention has the beneficial effects that: the visual transparent box body with the partition plate is adopted, and combined with the combined action of an electronic balance with scales, a compressive strength tester, a temperature sensor, a carbon dioxide concentration monitor, a heating rod, a supporting frame and the like, the visual transparent box body is used for testing the performance of the solid waste base foam concrete material and the capability of sealing and storing carbon dioxide; the method is used for researching the strength change of the solid waste base foam concrete in the process of sealing carbon dioxide, different initial fluidity, temperature and carbon dioxide pressure, and the influence on the sealing or curing of the solid waste base foam concrete, so as to find out the optimal parameter of the carbon dioxide which is completely cured in the solid waste base foam concrete material; the method has the advantages that the method is more intuitive, reliable, convenient, strong in contrast and strong in operability, and has important guiding significance for guiding safe and scientific exploitation of coal seams by researching the curing action process of the solid waste base foam concrete on carbon dioxide, the influence of the temperature difference of different buried coal rock layers on the curing stress of the solid waste base foam concrete and the supporting effect of the cured coal rock layers on the top plate, fully utilizing the underground waste space and effectively controlling the natural ignition danger of the goaf.|DRAWINGS DESCRIPTION|[0017] FIG. 1 is a schematic structural diagram of a test bed for testing the performance of solid waste base foam concrete materials and the capability of sealing carbon dioxide.|INVENTION MODE|Detailed Description|[0018] The invention will be further illustrated by the following examples in conjunction with the accompanying drawings:|[0019] a method for testing the performance and the carbon dioxide sequestration capacity of solid waste foam concrete comprises the following steps:|[0020] firstly, preparing a test bed for the performance of the solid waste base foam concrete material and the capability of sealing and storing carbon dioxide.|[0021] As shown in figure 1, the test bed for the performance and the capability of sealing carbon dioxide of the solid waste based foam concrete material mainly comprises a closed transparent box 1, a carbon dioxide steel cylinder 2, an electronic balance 3, a compressive strength tester 4, a temperature sensor 5, a carbon dioxide concentration monitor No. 1 6, a valve 8, a heating rod 9, a pipeline 10, a support frame 11 and a carbon dioxide concentration monitor No. 2 12.|[0022] A partition board 1a is arranged in the closed transparent box 1 to divide the space in the box into a left box body and a right box body, and the closed transparent box 1 and the partition board 1a are preferably made of acrylic plates.|[0023] An electronic balance 3 is fixedly arranged at the bottom of the closed transparent box 1, a left tray 3a and a right tray 3a of the electronic balance 3 respectively extend into the left box body and the right box body which respectively correspond to the left box body and the right box body, scale marks are drawn at the bottom of the trays 3a, and the trays 3a are preferably metal trays.|[0024] Each tray 3a is provided with a telescopic compressive strength tester 4 at the upper part and a telescopic supporting frame 11 at the lower part, and the supporting frame 10 can be the compressive strength tester 4, namely each tray 3a is provided with a telescopic compressive strength tester at the upper part and the lower part.|[0025] The left and right boxes are each provided with a temperature sensor 5 and a carbon dioxide concentration monitor No. 1 6. The bottom of the left box body and the bottom of the right box body are respectively provided with a heating rod 9 for heating the left box body and the right box body. The heating rods 9 are preferably uniformly laid on the bottoms of the left and right cases.|[0026] The left box body and the right box body are both provided with solid waste base foam concrete material inlets 7 for injecting solid waste base foam concrete materials into the trays 3a in the left box body and the right box body. The carbon dioxide steel cylinder 2 is connected with the left box body through a pipeline 10, and a No. 2 carbon dioxide concentration monitor 12 and a valve 8 are arranged on the pipeline 10. The carbon dioxide steel cylinder 2 is not connected with the right box body, one of the left box body and the right box body is filled with carbon dioxide, the other is not filled with carbon dioxide, and the left box body and the right box body are compared to accurately test the difference of the filled or not filled with carbon dioxide.|[0027] Preferably, a solid waste based foam concrete material inlet 7 and a connector connected with a pipeline 10 are arranged on the side walls of the left box body and the right box body, and the temperature sensor 5 and the No. 1 carbon dioxide concentration monitor 6 are arranged on the top of the left box body and the right box body.|[0028] In addition, the circumferential direction of the tray 3a is preferably provided with a surrounding edge, the size of the pressure head of the compressive strength tester 4 is matched with the size of the inner space of the circumferential surrounding edge of the tray 3a, and when the pressure head of the compressive strength tester 4 enters, the surrounding edge just covers the pressure head.|[0029] And secondly, injecting the same amount of foam concrete materials into the left tray 3a and the right tray 3a through solid waste base foam concrete material feed inlets 7 on the left box body and the right box body by the same injection equipment for sealing, wherein scales are drawn at the bottom of each tray 3a, and the initial fluidity of the sealing materials is judged by observing the diffusion distance of the sealing materials on the trays 3 a.|[0030] Thirdly, leveling the electronic balance 3, opening a valve 8 on the pipeline 10, and introducing a certain amount of carbon dioxide into the left box body; and observing data change of the electronic balance 3, temperature change monitored by the temperature sensors 5 of the left box body and the right box body and concentration change parameters monitored by the No. 1 carbon dioxide concentration monitor 6, so as to analyze the sealing amount of the foam concrete material to the carbon dioxide and the temperature evolution rule in the sealing process.|[0031] And fourthly, repeating the second step and the third step, raising the temperature of the left box body and the right box body to the same temperature through the heating rod 9, changing the injection pressure of the carbon dioxide through the valve 8 on the adjusting pipeline 10, observing the readings of the electronic balance 3, the temperature sensor 5 and the No. 1 carbon dioxide concentration monitor 6 again, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material.|[0032] And fifthly, after the sealing experiment is performed each time, lifting the supporting frame 11 to support the tray 3a, lowering the compression resistance experiment tester 4 to be in contact with the solid waste base foam concrete material in the tray 3a, gradually pressurizing the solidified solid waste base foam concrete material, testing the compression resistance strength of the solidified solid waste base foam concrete material and whether carbon dioxide overflows after the concrete material is crushed, judging whether the carbon dioxide is subjected to chemical reaction solidification or is physically sealed in the material, and simultaneously analyzing the influence of the carbon dioxide on the strength increase of the solid waste base foam concrete material.|[0033] In the pressurizing link of the experimental process, if carbon dioxide overflows from the crushed concrete material, the carbon dioxide is not completely cured in the solid waste-based foam concrete material and is temporarily stored, when the next experiment is repeated, the storage time can be prolonged or other parameters can be changed, the second step and the third step are repeated, and the second step and the third step are subjected to a plurality of storage tests until the optimal parameters of the carbon dioxide completely cured in the solid waste-based foam concrete material are found out. (CN113687055)|TECHNICAL FIELD|[0001] The invention relates to the technical field of solid waste base foam concrete performance test methods, and is used for testing the performance of solid waste base foam concrete materials and the capability of sealing carbon dioxide.|BACKGROUND ART|[0002] The solid waste base foam concrete mainly comprises solid waste base materials such as fly ash, carbide slag and the like. In the technical field of coal mining, the solid waste base foam concrete is used for sealing and curing carbon dioxide, so that the safety of coal mining can be ensured. However, the temperature difference of different buried depth coal rock layers is large, and the supporting effect of the top plate is different due to different sealed and solidified stresses. At present, no scientific research system and test method exists for the material performance of solid waste base foam concrete, and how to fully utilize underground waste space to carry out carbon dioxide sealing and curing and effectively manage the natural ignition danger of a goaf due to the influence of different temperatures and carbon dioxide injection pressures on the sealing and storing capacity of the foam concrete material.|DISCLOSURE|Disclosure of Invention|[0003] The invention aims to provide a method for testing the performance of a solid waste base foam concrete material and the capability of sealing carbon dioxide, which is used for researching the strength change of the solid waste base foam concrete in the process of sealing carbon dioxide, and the influence of different initial fluidity, temperature and carbon dioxide pressure on the sealing or curing of the solid waste base foam concrete.|[0004] Therefore, the technical scheme adopted by the invention is as follows: a method for testing the performance and the carbon dioxide sequestration capacity of solid waste foam concrete comprises the following steps:|[0005] firstly, preparing a test bed for the performance of a solid waste base foam concrete material and the capability of sealing and storing carbon dioxide;|[0006] the test bed for the performance and the capability of sealing and storing carbon dioxide of the solid waste base foam concrete material comprises a sealed transparent box and a carbon dioxide steel cylinder, a partition board is arranged in the sealed transparent box to divide the space in the box into a left box body and a right box body, an electronic balance is fixedly arranged at the bottom of the closed transparent box, a left tray and a right tray of the electronic balance respectively extend into the corresponding left box body and the corresponding right box body, scale marks are drawn at the bottoms of the trays, a telescopic compressive strength tester is arranged above each tray, a telescopic supporting frame is arranged below each tray, the left box body and the right box body are respectively provided with a temperature sensor and a carbon dioxide concentration monitor No. 1, heating rods are respectively arranged at the bottoms of the left box body and the right box body, solid waste base foam concrete material feeding ports are respectively arranged on the left box body and the right box body, carbon dioxide steel cylinders are connected with the left box body through pipelines, and the carbon dioxide concentration monitors No. 2 and valves are arranged on the pipelines;|[0007] secondly, injecting the same amount of foam concrete materials into left and right trays through solid waste base foam concrete material feed inlets on left and right box bodies for sealing and storing by the same pressure injection equipment, wherein scales are drawn at the bottom of each tray, and the initial fluidity of the sealing and storing material is judged by observing the diffusion distance of the sealing and storing material on the trays;|[0008] leveling an electronic balance, opening a valve on a pipeline, introducing a certain amount of carbon dioxide into the left box body, observing data change of the electronic balance, temperature change monitored by temperature sensors of the left box body and the right box body and concentration change parameters monitored by a carbon dioxide concentration monitor No. 1, and analyzing the sealing amount of the foam concrete material to the carbon dioxide and the temperature evolution rule in the sealing process;|[0009] fourthly, repeating the second step and the third step, raising the temperature of the left box body and the right box body to the same temperature through the heating rod, changing the injection pressure of the carbon dioxide through adjusting a valve on a pipeline, observing the readings of the electronic balance, the temperature sensor and the No. 1 carbon dioxide concentration monitor again, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material;|[0010] and fifthly, after the sealing experiment is performed each time, lifting the supporting frame to support the tray, lowering the compression resistance experiment tester to be in contact with the solid waste base foam concrete material in the tray, gradually pressurizing the solidified solid waste base foam concrete material, testing the compression resistance strength of the solidified solid waste base foam concrete material, and judging whether carbon dioxide overflows after the concrete material is crushed, so as to judge whether the carbon dioxide is subjected to chemical reaction solidification or is physically sealed in the material, and simultaneously analyzing the influence of the carbon dioxide on the strength increment of the solid waste base foam concrete material.|[0011] Preferably, the support frame is provided with a compressive strength tester.|[0012] Preferably, the solid waste base foam concrete material inlet and the interface connected with the pipeline are both arranged on the side walls of the left box body and the right box body.|[0013] More preferably, the heating rods are uniformly laid at the bottoms of the left box body and the right box body, and the temperature sensors and the No. 1 carbon dioxide concentration monitors are arranged at the tops of the left box body and the right box body.|[0014] Further preferably, the circumference of the tray is provided with a surrounding edge, and the size of the pressure head of the compressive strength tester is matched with the size of the inner space of the circumferential surrounding edge of the tray.|[0015] Preferably, the closed transparent box and the partition plate are both made of acrylic plates, and the tray is a metal tray.|[0016] The invention has the beneficial effects that: the visual transparent box body with the partition plate is adopted, and combined with the combined action of an electronic balance with scales, a compressive strength tester, a temperature sensor, a carbon dioxide concentration monitor, a heating rod, a supporting frame and the like, the visual transparent box body is used for testing the performance of the solid waste base foam concrete material and the capability of sealing and storing carbon dioxide; the method is used for researching the strength change of the solid waste base foam concrete in the process of sealing carbon dioxide, different initial fluidity, temperature and carbon dioxide pressure, and the influence on the sealing or curing of the solid waste base foam concrete, so as to find out the optimal parameter of the carbon dioxide which is completely cured in the solid waste base foam concrete material; the method has the advantages that the method is more intuitive, reliable, convenient, strong in contrast and strong in operability, and has important guiding significance for guiding safe and scientific exploitation of coal seams by researching the curing action process of the solid waste base foam concrete on carbon dioxide, the influence of the temperature difference of different buried coal rock layers on the curing stress of the solid waste base foam concrete and the supporting effect of the cured coal rock layers on the top plate, fully utilizing the underground waste space and effectively controlling the natural ignition danger of the goaf.|DRAWINGS DESCRIPTION|[0017] FIG. 1 is a schematic structural diagram of a test bed for testing the performance of solid waste base foam concrete materials and the capability of sealing carbon dioxide.|INVENTION MODE|Detailed Description|[0018] The invention will be further illustrated by the following examples in conjunction with the accompanying drawings:|[0019] a method for testing the performance and the carbon dioxide sequestration capacity of solid waste foam concrete comprises the following steps:|[0020] firstly, preparing a test bed for the performance of the solid waste base foam concrete material and the capability of sealing and storing carbon dioxide.|[0021] As shown in figure 1, the test bed for the performance and the capability of sealing carbon dioxide of the solid waste based foam concrete material mainly comprises a closed transparent box 1, a carbon dioxide steel cylinder 2, an electronic balance 3, a compressive strength tester 4, a temperature sensor 5, a carbon dioxide concentration monitor No. 1 6, a valve 8, a heating rod 9, a pipeline 10, a support frame 11 and a carbon dioxide concentration monitor No. 2 12.|[0022] A partition board 1a is arranged in the closed transparent box 1 to divide the space in the box into a left box body and a right box body, and the closed transparent box 1 and the partition board 1a are preferably made of acrylic plates.|[0023] An electronic balance 3 is fixedly arranged at the bottom of the closed transparent box 1, a left tray 3a and a right tray 3a of the electronic balance 3 respectively extend into the left box body and the right box body which respectively correspond to the left box body and the right box body, scale marks are drawn at the bottom of the trays 3a, and the trays 3a are preferably metal trays.|[0024] Each tray 3a is provided with a telescopic compressive strength tester 4 at the upper part and a telescopic supporting frame 11 at the lower part, and the supporting frame 10 can be the compressive strength tester 4, namely each tray 3a is provided with a telescopic compressive strength tester at the upper part and the lower part.|[0025] The left and right boxes are each provided with a temperature sensor 5 and a carbon dioxide concentration monitor No. 1 6. The bottom of the left box body and the bottom of the right box body are respectively provided with a heating rod 9 for heating the left box body and the right box body. The heating rods 9 are preferably uniformly laid on the bottoms of the left and right cases.|[0026] The left box body and the right box body are both provided with solid waste base foam concrete material inlets 7 for injecting solid waste base foam concrete materials into the trays 3a in the left box body and the right box body. The carbon dioxide steel cylinder 2 is connected with the left box body through a pipeline 10, and a No. 2 carbon dioxide concentration monitor 12 and a valve 8 are arranged on the pipeline 10. The carbon dioxide steel cylinder 2 is not connected with the right box body, one of the left box body and the right box body is filled with carbon dioxide, the other is not filled with carbon dioxide, and the left box body and the right box body are compared to accurately test the difference of the filled or not filled with carbon dioxide.|[0027] Preferably, a solid waste based foam concrete material inlet 7 and a connector connected with a pipeline 10 are arranged on the side walls of the left box body and the right box body, and the temperature sensor 5 and the No. 1 carbon dioxide concentration monitor 6 are arranged on the top of the left box body and the right box body.|[0028] In addition, the circumferential direction of the tray 3a is preferably provided with a surrounding edge, the size of the pressure head of the compressive strength tester 4 is matched with the size of the inner space of the circumferential surrounding edge of the tray 3a, and when the pressure head of the compressive strength tester 4 enters, the surrounding edge just covers the pressure head.|[0029] And secondly, injecting the same amount of foam concrete materials into the left tray 3a and the right tray 3a through solid waste base foam concrete material feed inlets 7 on the left box body and the right box body by the same injection equipment for sealing, wherein scales are drawn at the bottom of each tray 3a, and the initial fluidity of the sealing materials is judged by observing the diffusion distance of the sealing materials on the trays 3 a.|[0030] Thirdly, leveling the electronic balance 3, opening a valve 8 on the pipeline 10, and introducing a certain amount of carbon dioxide into the left box body; and observing data change of the electronic balance 3, temperature change monitored by the temperature sensors 5 of the left box body and the right box body and concentration change parameters monitored by the No. 1 carbon dioxide concentration monitor 6, so as to analyze the sealing amount of the foam concrete material to the carbon dioxide and the temperature evolution rule in the sealing process.|[0031] And fourthly, repeating the second step and the third step, raising the temperature of the left box body and the right box body to the same temperature through the heating rod 9, changing the injection pressure of the carbon dioxide through the valve 8 on the adjusting pipeline 10, observing the readings of the electronic balance 3, the temperature sensor 5 and the No. 1 carbon dioxide concentration monitor 6 again, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material.|[0032] And fifthly, after the sealing experiment is performed each time, lifting the supporting frame 11 to support the tray 3a, lowering the compression resistance experiment tester 4 to be in contact with the solid waste base foam concrete material in the tray 3a, gradually pressurizing the solidified solid waste base foam concrete material, testing the compression resistance strength of the solidified solid waste base foam concrete material and whether carbon dioxide overflows after the concrete material is crushed, judging whether the carbon dioxide is subjected to chemical reaction solidification or is physically sealed in the material, and simultaneously analyzing the influence of the carbon dioxide on the strength increase of the solid waste base foam concrete material.|[0033] In the pressurizing link of the experimental process, if carbon dioxide overflows from the crushed concrete material, the carbon dioxide is not completely cured in the solid waste-based foam concrete material and is temporarily stored, when the next experiment is repeated, the storage time can be prolonged or other parameters can be changed, the second step and the third step are repeated, and the second step and the third step are subjected to a plurality of storage tests until the optimal parameters of the carbon dioxide completely cured in the solid waste-based foam concrete material are found out. Family Number|(97173977)|97173977|Abstract|(CN113687055 A)|The invention discloses a method for testing the performance and carbon dioxide storage capacity of solid waste - based foam concrete . The method comprises the following steps : 1, preparing a solid waste - based foam concrete material performance and carbon dioxide storage capacity test bed ; 2, injecting the same amount of foam concrete material into a left tray and a right tray for sealing ; 3, introducing carbon dioxide into a left box body , and analyzing the storage amount of the foam concrete material on the carbon dioxide and the temperature evolution rule in the storage process ; 4, repeating the second step and the third step , and analyzing the influence of the initial fluidity , the temperature and the injection pressure on the sealing capacity of the foam concrete material ; and 5, testing the compressive strength of the solid waste - based foam concrete material after curing , and testing whether carbon dioxide overflows after the concrete material is crushed . The method is used for researching the strength change of the solid waste - based foam concrete in the carbon dioxide sealing process and the influence of different initial fluidity , temperature and carbon dioxide pressure on the sealing or curing of the solid waste - based foam concrete . |CPC codes|(CN113687055 A)|G01D - 021/02 |G01N - 003/08 |G01N - 033/38/3 |G01N - 2203/0019 |IPC codes|(CN113687055 A)|G01D - 021/02 |G01N - 003/08 |G01N - 033/38 |Title|(CN113687055 A)|Method for testing performance and carbon dioxide sequestration capacity of solid waste - based foam concrete | Analysis of biological materials G01D-021/02|G01N-003/08|G01N-033/38/3|G01N-2203/0019 G01D-021/02|G01N-003/08|G01N-033/38/3|G01N-2203/0019 G01D-021/02|G01N-003/08|G01N-033/38 G01D-021/02|G01N-003/08|G01N-033/38 CN114180889 CN114180889 99104484 WHO=Examiner SELF=Y CAT=Y LAPSED (CN113687055)|LAPSED DEAD (CN113687055)|DEAD (CN113687055)|LEGAL DETAILS FOR CN113687055|Actual or expected expiration date=2023-09-01|Legal state=DEAD|Status=LAPSED|Event publication date=2021-09-30|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202111157076|Application date=2021-09-30|Standardized application number=2021CN-1157076|Event publication date=2021-11-23|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN113687055|Publication stage code=A|Publication date=2021-11-23|Standardized publication number=CN113687055|Event publication date=2021-11-23|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2021-12-10|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-09-01|Event code=CN/WW01|Event indicator=Neg|Event group=Event indicating Not In Force|Withdrawal of patent application after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQc6OHda98XNlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000059992327&ekey=2188&xpn=CN113687055&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=sQTTvGhCWdBFQ4mVj52wf5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN113687055)|CN (CN113687055)|NAME=SHANDONG UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN113687055)|NAME=TAN XIAORONG;CHONGQING TIANCHENGHZUOYUE PATENT AGENCY (GENERAL PARTNERSHIP) , REG=50240 (CN113687055)|NAME=SUN LULU|NAME=DUAN SHOULEI|NAME=WANG GANG|NAME=WANG HAISHAN|NAME=CAO XIAOQIANG|NAME=XIN LIN 0 1 Titre: (CN113687055)|Method for testing performance and carbon dioxide sequestration capacity of solid waste-based foam concrete Résumé: (CN113687055)|The invention discloses a method for testing the performance and carbon dioxide storage capacity of solid waste-based foam concrete. The method comprises the following steps: 1, preparing a solid waste-based foam concrete material performance and carbon dioxide storage capacity test bed; 2, injecting the same amount of foam concrete material into a left tray and a right tray for sealing; 3, introducing carbon dioxide into a left box body, and analyzing the storage amount of the foam concrete material on the carbon dioxide and the temperature evolution rule in the storage process; 4, repeating the second step and the third step, and analyzing the influence of the initial fluidity, the temperature and the injection pressure on the sealing capacity of the foam concrete material; and 5, testing the compressive strength of the solid waste-based foam concrete material after curing, and testing whether carbon dioxide overflows after the concrete material is crushed. The method is used for researching the strength change of the solid waste-based foam concrete in the carbon dioxide sealing process and the influence of different initial fluidity, temperature and carbon dioxide pressure on the sealing or curing of the solid waste-based foam concrete. 112 Abstract gpt-4o-mini no The article focuses on testing the carbon dioxide storage capacity of foam concrete made from solid waste, which does not involve accelerated weathering or mineral carbonation processes related to silicate or alkaline minerals.
114 CN202220240693U CN202220240693U CN217549273 102093066 CN217549273 U 2022-10-11 [CN217549273U] 2022-01-28 2022-01-28 2022-10-11 (CN217549273U)|2022-10-11 (CN217549273)|2032-01-28 (CN217549273)|Coal chemical solid waste gas and waste comprehensive utilization system (CN217549273)|The utility model provides a coal chemical solid waste gas and waste comprehensive utilization system. The system module comprises a flue gas dust removal module, a carbon capture module, a desorption module, a desulfurization and denitrification module, a solid waste raw material pretreatment module, a grinding and briquetting module and a mineralization reaction module which are sequentially and fixedly connected through pipelines. Flue gas enters the system from a gas inlet of the bag-type dust removal device, dust particles are subjected to dust removal through a dust removal bag to obtain corresponding impurity-removed flue gas, the impurity-removed flue gas flows out from a gas outlet, the impurity-removed flue gas enters a carbon removal capture tower, carbon dioxide in the flue gas is captured and absorbed, and then absorption liquid flows back to a storage tank; the flue gas after carbon capture enters a desulfurization and denitrification tower, is desulfurized and denitrified through a calcium carbide layer, and then is discharged from an exhaust port, desulfurization slag and carbide slag used by the desulfurization and denitrification tower are conveyed to a weighing device to be mixed, preliminarily crushed and weighed, and then mixed powder is conveyed to a briquetting machine to be mixed with a small amount of cement to be subjected to briquetting so as to prepare a pressed part. JIANGSU JICUI FUNCTIONAL MATERIALS RESEARCH INSTITUTE (CN217549273)|JIANGSU JICUI FUNCTIONAL MATERIALS RESEARCH INSTITUTE CO., LTD. ([CN]) CHENG MINGZHAO|LI YI|REN TIANBIN|JING ZHENZI|LI CHEN (CN217549273)|CHENG MINGZHAO|LI YI|REN TIANBIN|JING ZHENZI|LI CHEN (CN217549273)|1. the utility model provides a useless comprehensive utilization system of solid waste gas of coal chemical industry can be through the synergism of a plurality of modules to realize the reutilization of the solid waste gas waste material in coal chemical industry field, and can realize the useless pair of processing of solid useless gas in the use of system, thereby improve system efficiency.|The carbide slag has fine particle size and high reaction activity, is mainly used for replacing limestone to prepare building and construction materials such as cement and the like by traditional large-scale consumption, but is limited by saturation of domestic markets, centralized geographic positions and the like; the main component of the carbide slag is calcium hydroxide which can be used for preparing chemical products such as calcium oxide, calcium carbonate and the like, but the treatment process is high in cost and easy to cause secondary pollution due to the influence of impurities in the carbide slag; the carbide slag is strongly alkaline, has better ablation property, has excellent performance in the environmental treatment processes of acid wastewater, flue gas desulfurization and the like, replaces a calcium-based absorbent for flue gas desulfurization, and becomes one of the development directions of comprehensive utilization of the carbide slag.| (CN217549273)|1. The utility model provides a useless comprehensive utilization system of coal industry solid waste gas which characterized in that: the system module comprises a flue gas dust removal module (1), a carbon capture module (2), a desorption module (3), a desulfurization and denitrification module (4), a solid waste raw material pretreatment module (5), a grinding and briquetting module (6) and a mineralization reaction module (7); the flue gas dust removal module (1) is a cloth bag dust removal device; the cloth bag dust removal device comprises a moving part (8), an air inlet (9), an air outlet (10), a dust removal cloth bag (11) and a dust discharge hole (14); the moving part (8) is fixed on one side of the top of the bag-type dust collector, and the moving part (8) comprises moving wheels and an output shaft (12) extending towards the inside of a box body of the moving part (8); 3-6 injection pipes (13) are further fixed on the output shaft (12), and the injection pipes (13) are mechanically and fixedly connected with the output shaft (12) through fixing pins; the air inlet (9) is positioned in the middle of the box body of the cloth bag dust removal device and used for allowing flue gas to enter, and the air outlet (10) is positioned at the top of the box body of the cloth bag dust removal device and used for discharging the flue gas after dust removal; the dust discharge hole (14) is positioned at the bottom of a box body of the cloth bag dust removal device and used for discharging dust, and then dust is collected; the carbon capture module (2) is a carbon capture absorption device; the desorption module (3) is a carbon capture desorption device; the carbon capture absorption device comprises a carbon capture absorption tower (15); a liquid storage tank (16) is also arranged at the bottom of the carbon capture absorption tower (15), and the liquid storage tank (16) is fixedly connected with an air outlet (10) of the cloth bag dust removal device through a pipeline; the carbon capture and absorption device is also provided with a circulating storage tank (17) for carbon capture liquid; the circulating storage tank (17) is fixedly connected with the bottom end and the top of the carbon capturing and absorbing tower (15) through pipelines, and a liquid inlet pump is arranged in a fixed pipeline connected with the top of the circulating storage tank and used for conveying the carbon capturing liquid to the top of the carbon capturing and absorbing tower (15); the carbon capture liquid returns to the circulating storage tank (17) through an outlet at the bottom end after being used; the carbon capture desorption device comprises a carbon capture desorption tower (19), a gas storage tank (20) and a reflux tank (18); the top of the carbon capturing and desorbing tower (19) and the reflux groove (18) at the bottom end are fixedly connected with the circulating storage tank (17) through pipelines, and the carbon capturing and desorbing tower (19) is fixedly connected with the gas storage tank (20) through pipelines; the desulfurization and denitrification module (4) is a desulfurization and denitrification tower (21); the bottom of the desulfurization and denitrification tower (21) is fixedly connected with a top pipeline of the carbon capture absorption tower (15), and an exhaust port (22) is formed in the top of the desulfurization and denitrification tower (21) and used for exhausting flue gas subjected to desulfurization and denitrification; 5-20 carbide slag layers are arranged in the desulfurization and denitrification tower (21).| (CN217549273)|In order to solve the problems, the invention provides a coal chemical industry solid waste gas and waste gas comprehensive utilization system, and the system modules comprise a flue gas dust removal module 1, a carbon capture module 2, a desorption module 3, a desulfurization and denitrification module 4, a solid waste raw material pretreatment module 5, a grinding and briquetting module 6 and a mineralization reaction module 7.|The application provides a comprehensive utilization system for solid waste gas and waste gas in coal chemical industry,the adopted solid waste and gas waste raw materials can be obtained from local materials in chemical plants and the like, the solid waste is simply treated and directly pressed into building materials, and the trapped high-concentration CO is 2 Reacts with the massive building materials to obtain the building materials with the strength meeting the building requirements, thereby really realizing CO 2 The net emission reduction and the direct production of the product building materials from the coal chemical industry plant, but not the building material raw materials, the whole process has low energy consumption and small emission.| (CN217549273)|SOLID WASTE(100,32)|CHEMICAL INDUSTRY(100,17)|COAL CHEMICAL INDUSTRY(100,17)|EXTENSIVE UTILIZATION(100,14)|SOLID WASTE GAS(100,11)|GAS(100,5)|USELESS COMPREHENSIVE UTILIZATION(100,5)|COAL INDUSTRY(100,3)|COAL INDUSTRY SOLID WASTE(100,3)|DENITRIFICATION TOWER(86,18)|CARBIDE SLAG(79,7)|DENITRIFICATION MODULE(72,7)|CARBIDE SLAG COMPREHENSIVE UTILIZATION(71,1)|DESORPTION MODULE(65,7)|BRIQUETTING MODULE(63,6)|MINERALIZATION REACTION MODULE(61,7)|CLOTH BOX(59,5)|DESULFURIZATION(55,22)|MINERALIZATION REACTION KETTLE(49,10)|MODULE SYNERGISM(46,1)|BRIQUETTING BOX(44,12)|DESULFURIZATION SEDIMENT(42,1)|CARBON CAPTURE ABSORPTION TOWER(39,13)|DESULFURIZATION ASH RESIDUE(39,1)|STORAGE TANK CIRCULATION(38,15)|CALCIUM ABSORBENT(36,1)|DOMESTIC MARKET SATURATION(36,1)|DESORBING CARBON CAPTURE(35,5)|CARBIDE SLAG COMPONENT(35,1)|REFLUX TANK(35,1)|PIPELINE(34,10)|CARBON CAPTURE MODULE(34,8)|CARBIDE SEDIMENT(34,1)|PRELIMINARY CRUSHING(33,1)|TOWER(31,10)|BAG DUST COLLECTOR(30,10)|GRINDING(30,10)|BUILDING REQUIREMENT(30,1)|DUST REMOVAL MODULE(29,8)|CARBON CAPTURE DESORPTION TOWER(29,6)|BRIQUETTED WORKPIECE(28,3)|WASTE CARBIDE SLAG(28,3)|ACIDIC WASTEWATER(28,1)|WASTE GAS COMPREHENSIVE UTILIZATION(28,1)|DUST REMOVAL(27,16)|BRIQUETTING MACHINE(27,5)|CLOTH BAG(27,3)|FLUE GAS(26,31)|ABSORBING CARBON CAPTURE(26,6)|DUST DISCHARGE(25,2)|DUST REMOVAL CLOTH BAG(25,2)|REUTILIZATION(25,1)|CLOTH BAG DUST REMOVAL(24,3)|REFLUX GROOVE(24,3)|DENITRIFICATION(24,2)|ASH RESIDUE DISCHARGE(24,1)|CARBON ENTRAPMENT(24,1)|CONTAMINATION(23,1)|DESULFURIZATION TOP(23,1)|LATE DISCHARGE(23,1)|STORAGE BOX(22,6)|FIXED PIPELINE(22,4)|ABRASIVE COMPACT MODULE(22,3)|MIXING CARBIDE SLAG(22,3)|ASH RESIDUE FEED PORT(22,1)|RAW MATERIAL PRETREATMENT MODULE(21,11)|CLOTH(21,5)|CEMENT(21,3)|INJECTION PIPE(21,2)|AIR INLET(20,4)|WEIGHED ASH(20,3)|LIMESTONE(20,1)|NET EMISSION REDUCTION(20,1)|DUST(19,11)|DESULFURIZATION BOTTOM(19,3)|FLUE GAS DESULFURIZATION(19,2)|ABLATION(19,1)|SOLID USELESS GAS(19,1)|CARBON TOP(18,5)|FIXING PIN(18,3)|DUST PARTICLE(18,2)|DOMESTIC MARKET(18,1)|LIQUID RETURN(18,1)|CARBON CAPTURE LIQUID RETURN(17,1)|GAS VENT(17,1)|TOP PIPELINE(17,1)|WASTE GAS(16,5)|FEEDING MIXED ASH(16,3)|LIQUID INLET PUMP(16,3)|CARBIDE LAYER(16,1)|SOLID WASTE ADOPTION(16,1)|SYSTEM MODULE(15,4)|MOVING WHEEL(15,3)|SOX NOX CONTROL TOWER(15,2)|DUST REMOVAL BAG(15,1)|DUST COLLECTOR(14,10)|CARBON CAPTURE(14,9)|BRIQUETTING PLATE(14,3)|CALCIUM CARBONATE(14,1)|CALCIUM HYDROXIDE(14,1)|FEED HOLE(14,1)|GEOGRAPHIC POSITION CENTRALIZATION(14,1)|REMOVING CARBON(14,1)|GAS STORAGE TANK(13,8)|MIXED POWDER(13,2)|DEVELOPMENT DIRECTION(13,1)|LIQUID STORAGE TANK(12,6)|CARBIDE(12,5)|COMPACT PRESS(12,3)|SMALL EMISSION(12,1)|AIR OUTLET(11,8)|GAS OUTLET(11,4)|BUILDING MATERIAL(10,6)|IMPURITY REMOVED FLUE GAS(10,6)|CARBON CAPTURE LIQUID(10,5)|EXHAUST PORT(10,5)|CALCIUM OXIDE(10,1)|CHEMICAL PLANT(10,1)|COMPREHENSIVE UTILIZATION MINERALIZATION REACTOR(10,1)|ENERGY CONSUMPTION(10,1)|MASSIVE BUILDING MATERIAL(10,1)|ROTATING PUSH ROD(10,1)|OUTPUT SHAFT(9,10)|GAS INLET(9,4)|SLAG MASS(9,2)|BLOWING PIPE(8,5)|CIRCULATING STORAGE TANK TOP(8,3)|WEIGHING SCALE(8,2)|FINE PARTICLE SIZE(8,1)|MASS CONSUMPTION(8,1)|RAW MATERIAL RESIDUE(8,1)|AUTOCLAVE NUMBER(7,3)|CATEGORIZED B01D(7,1)|CHEMICAL PRODUCT(7,1)|DESULFURIZATION ASH MIXING(7,1)|GAS WASTE RAW MATERIAL(7,1)|GRINDING BRIQUETTING MODULE(7,1)|DENITRATION TOWER(6,1)|DESULFURIZATION ADOPTION(6,1)|DUST COLLECTING BAG(6,1)|GAS WASTE MATERIAL(6,1)|PRODUCT BUILDING MATERIAL(6,1)|PRODUCT BUILDING MATERIAL PRODUCTION(6,1)|SLAG GASIFICATION(6,1)|ABSORBING LIQUID FLOW(5,2)|COAL GANGUE(5,1)|COAL SLIME(5,1)|DENITRATION MODULE(5,1)|DESORPTION TOWER(5,1)|GASIFIED FLY ASH(5,1)|POWDER PRETREATMENT MODULE(5,1)| (CN217549273)|1. The utility model provides a useless comprehensive utilization system of coal industry solid waste gas which characterized in that: the system module comprises a flue gas dust removal module (1), a carbon capture module (2), a desorption module (3), a desulfurization and denitrification module (4), a solid waste raw material pretreatment module (5), a grinding and briquetting module (6) and a mineralization reaction module (7);|the flue gas dust removal module (1) is a cloth bag dust removal device; the cloth bag dust removal device comprises a moving part (8), an air inlet (9), an air outlet (10), a dust removal cloth bag (11) and a dust discharge hole (14); the moving part (8) is fixed on one side of the top of the bag-type dust collector, and the moving part (8) comprises moving wheels and an output shaft (12) extending towards the inside of a box body of the moving part (8); 3-6 injection pipes (13) are further fixed on the output shaft (12), and the injection pipes (13) are mechanically and fixedly connected with the output shaft (12) through fixing pins; the air inlet (9) is positioned in the middle of the box body of the cloth bag dust removal device and used for allowing flue gas to enter, and the air outlet (10) is positioned at the top of the box body of the cloth bag dust removal device and used for discharging the flue gas after dust removal; the dust discharge hole (14) is positioned at the bottom of a box body of the cloth bag dust removal device and used for discharging dust, and then dust is collected;|the carbon capture module (2) is a carbon capture absorption device; the desorption module (3) is a carbon capture desorption device; the carbon capture absorption device comprises a carbon capture absorption tower (15); a liquid storage tank (16) is also arranged at the bottom of the carbon capture absorption tower (15), and the liquid storage tank (16) is fixedly connected with an air outlet (10) of the cloth bag dust removal device through a pipeline; the carbon capture and absorption device is also provided with a circulating storage tank (17) for carbon capture liquid; the circulating storage tank (17) is fixedly connected with the bottom end and the top of the carbon capturing and absorbing tower (15) through pipelines, and a liquid inlet pump is arranged in a fixed pipeline connected with the top of the circulating storage tank and used for conveying the carbon capturing liquid to the top of the carbon capturing and absorbing tower (15); the carbon capture liquid returns to the circulating storage tank (17) through an outlet at the bottom end after being used;|the carbon capture desorption device comprises a carbon capture desorption tower (19), a gas storage tank (20) and a reflux tank (18); the top of the carbon capturing and desorbing tower (19) and the reflux groove (18) at the bottom end are fixedly connected with the circulating storage tank (17) through pipelines, and the carbon capturing and desorbing tower (19) is fixedly connected with the gas storage tank (20) through pipelines;|the desulfurization and denitrification module (4) is a desulfurization and denitrification tower (21); the bottom of the desulfurization and denitrification tower (21) is fixedly connected with a top pipeline of the carbon capture absorption tower (15), and an exhaust port (22) is formed in the top of the desulfurization and denitrification tower (21) and used for exhausting flue gas subjected to desulfurization and denitrification; 5-20 carbide slag layers are arranged in the desulfurization and denitrification tower (21).|2. The comprehensive utilization system for solid waste gas in coal chemical industry according to claim 1, characterized in that: the solid waste raw material pretreatment module (5) comprises a powder weighing device; the powder weighing device is used for measuring and weighing the waste carbide slag and the desulfurization ash slag left in the desulfurization and denitrification tower (21); the solid waste raw material pretreatment module (5) also comprises a crushing device for primarily crushing weighed ash.|3. The comprehensive utilization system for solid waste gas in coal chemical industry according to claim 2, characterized in that: the powder weighing device comprises an ash feeding hole (23), a storage box (24), a handle (30), an ash discharging hole (29), a base (31) and a weighing table (25); the handles (30) and the ash residue discharge ports (29) are respectively arranged at two opposite sides of the storage box (24), and the ash residue feed port (23) is arranged at the top end of the storage box (24) and used for feeding and mixing carbide slag and desulfurization ash residue; the storage box (24) is detachably and fixedly connected to the top end of the base (31), and the base (31) comprises a weighing scale (25) for displaying the ash and slag mass value.|4. The comprehensive utilization system for solid waste gas and waste gas in coal chemical industry according to claim 3, characterized in that: the abrasive compact module (6) comprises a compact press; the briquetting machine comprises a briquetting box body (26), and a feeding hole (32) for feeding mixed ash is formed in the top end of the briquetting box body (26); the left end of the briquetting box body (26) is provided with a rotating push rod (28) for driving the briquetting plate (27) on the same side in the briquetting box body (26) to extrude towards the other side; the grinding and briquetting module (6) also comprises a grinding device used for grinding the briquetted workpieces.|5. The comprehensive utilization system for solid waste gas and waste gas in coal chemical industry according to claim 4, characterized in that: the mineralization reaction module (7) is a mineralization reaction kettle; the mineralization reaction kettle is a continuous mineralization reaction kettle which is formed by connecting autoclaves (33) in series and/or in parallel.|6. The comprehensive utilization system for solid waste gas and waste gas in coal chemical industry according to claim 5, characterized in that: the number of the autoclaves (33) is 5-20. (CN217549273)|TECHNICAL FIELD|[0001] The utility model belongs to the categorised B01D53/00 field of patent IPC, more specifically relates to a useless comprehensive utilization system of coal industry solid waste gas.|BACKGROUND ART|[0002] The coal chemical industry solid waste comprises gasified fly ash, gasified slag, coal slime, coal gangue, fly ash and the like, compounds containing silicon, aluminum, magnesium, iron and calcium, and a small amount of titanium, potassium, sodium, phosphorus and the like. In recent years, the utilization of industrial waste residues as raw materials of brickworks is a research hotspot in the field of solid waste treatment, so that the utilization rate of solid waste can be improved, the use of raw materials adopted by buildings can be saved, and the effects of energy conservation and emission reduction are achieved. The carbide slag is industrial waste slag formed after acetylene gas is produced by using carbide, and causes pollution to the environment. The carbide slag has fine particle size and high reaction activity, is mainly used for replacing limestone to prepare building and construction materials such as cement and the like by traditional large-scale consumption, but is limited by saturation of domestic markets, centralized geographic positions and the like; the main component of the carbide slag is calcium hydroxide which can be used for preparing chemical products such as calcium oxide, calcium carbonate and the like, but the treatment process is high in cost and easy to cause secondary pollution due to the influence of impurities in the carbide slag; the carbide slag is strongly alkaline, has better ablation property, has excellent performance in the environmental treatment processes of acid wastewater, flue gas desulfurization and the like, replaces a calcium-based absorbent for flue gas desulfurization, and becomes one of the development directions of comprehensive utilization of the carbide slag.|[0003] Therefore, the utility model provides a pair of make full use of in the coal chemical industry solid useless and useless comprehensive utilization system of gas to solve waste pollution and the problem that the utilization of the solid gas of coal chemical industry received the restriction.|DISCLOSURE|SUMMERY OF THE UTILITY MODEL|[0004] In order to solve the problems, the invention provides a coal chemical industry solid waste gas and waste gas comprehensive utilization system, and the system modules comprise a flue gas dust removal module 1, a carbon capture module 2, a desorption module 3, a desulfurization and denitrification module 4, a solid waste raw material pretreatment module 5, a grinding and briquetting module 6 and a mineralization reaction module 7.|[0005] As a preferred scheme, the flue gas dust removal module 1 is a cloth bag dust removal device; the cloth bag dust removal device comprises a moving part 8, an air inlet 9, an air outlet 10, a dust removal cloth bag 11 and a dust discharge hole 14; the moving part 8 is fixed on one side of the top of the bag-type dust collector, and the moving part 8 comprises moving wheels and an output shaft 12 extending towards the interior of the box body of the moving part 8; 3-6 blowing pipes 13 are further fixed on the output shaft 12, and the blowing pipes 13 are mechanically and fixedly connected with the output shaft 12 through fixing pins; the gas inlet 9 is positioned in the middle of the box body of the bag-type dust collector and used for allowing the flue gas to enter, and the gas outlet 10 is positioned at the top of the box body of the bag-type dust collector and used for discharging the flue gas after dust removal; the dust discharge hole 14 is located at the bottom of a box body of the cloth bag dust removal device and used for discharging dust, and then collecting the dust.|[0006] As a preferable mode, the carbon capture module 2 is a carbon capture absorption device; the desorption module 3 is a carbon capture desorption device; the carbon capture absorption device includes a carbon capture absorption tower 15; a liquid storage tank 16 is also arranged at the bottom of the carbon capture absorption tower 15, and the liquid storage tank 16 is fixedly connected with a pipeline of an air outlet 10 of the cloth bag dust removal device; the carbon capture and absorption device is also provided with a circulating storage tank 17 for carbon capture liquid; the circulating storage tank 17 is fixedly connected with the bottom end and the top of the carbon capture absorption tower 15 through pipelines, and a liquid inlet pump is arranged in a fixed pipeline connected with the top of the circulating storage tank and used for conveying the carbon capture liquid to the top of the carbon capture absorption tower 15; the carbon capture liquid is returned to the recycle storage tank 17 through an outlet at the bottom end after use.|[0007] As a preferable scheme, the carbon capture and desorption device comprises a carbon capture and desorption tower 19, a gas storage tank 20 and a reflux groove 18; the top of the carbon capture desorption tower 19 and the reflux groove 18 at the bottom are fixedly connected with the circulating storage tank 17 through pipelines, and the carbon capture desorption tower 19 and the gas storage tank 20 are fixedly connected through pipelines.|[0008] As a preferable scheme, the desulfurization and denitrification module 4 is a desulfurization and denitrification tower 21; the bottom of the desulfurization and denitrification tower 21 is fixedly connected with a top end pipeline of the carbon capture absorption tower 15, and an exhaust port 22 is arranged at the top end of the desulfurization and denitrification tower 21 and used for discharging desulfurized and denitrated flue gas; 5-20 carbide slag layers are arranged in the desulfurization and denitrification tower 21.|[0009] As a preferable scheme, the solid waste raw material pretreatment module 5 comprises a powder weighing device; the powder weighing device is used for measuring and weighing the waste carbide slag and the desulfurization ash slag left in the desulfurization and denitrification tower 21; the solid waste raw material pretreatment module 5 also comprises a crushing device for primarily crushing the weighed ash.|[0010] As a preferable scheme, the powder weighing device comprises an ash inlet 23, a storage box 24, a handle 30, an ash outlet 29, a base 31 and a weighing meter 25; the handle 30 and the ash discharging port 29 are respectively arranged at two opposite sides of the storage box 24, and the ash feeding port 23 is arranged at the top end of the storage box 24 and used for feeding and mixing carbide slag and desulfurization ash; the storage box 24 is detachably and fixedly connected to the top end of a base 31, and the base 31 comprises a weighing meter 25 for displaying the ash and slag mass value.|[0011] As a preferred solution, the abrasive compact module 6 comprises a compact press; the briquetting machine comprises a briquetting box 26, and a feed inlet 32 is formed in the top end of the briquetting box 26 and used for feeding mixed ash; a rotary push rod 28 is arranged at the left end of the briquetting box body 26 and is used for driving the briquetting plate 27 on the same side in the briquetting box body 26 to extrude towards the other side; the grinding and briquetting module 6 also comprises a grinding device for grinding the briquetted workpieces.|[0012] As a preferred scheme, the mineralization reaction module 7 is a mineralization reaction kettle; the mineralization reaction kettle is a continuous mineralization reaction kettle which is formed by connecting autoclaves 33 in series and/or in parallel.|[0013] In a preferred embodiment, the number of the autoclaves 33 is 5 to 20.|[0014] Has the advantages that:|[0015] 1. the utility model provides a useless comprehensive utilization system of solid waste gas of coal chemical industry can be through the synergism of a plurality of modules to realize the reutilization of the solid waste gas waste material in coal chemical industry field, and can realize the useless pair of processing of solid useless gas in the use of system, thereby improve system efficiency.|[0016] 2. The application provides a comprehensive utilization system for solid waste gas and waste gas in coal chemical industry,the adopted solid waste and gas waste raw materials can be obtained from local materials in chemical plants and the like, the solid waste is simply treated and directly pressed into building materials, and the trapped high-concentration CO is 2 Reacts with the massive building materials to obtain the building materials with the strength meeting the building requirements, thereby really realizing CO 2 The net emission reduction and the direct production of the product building materials from the coal chemical industry plant, but not the building material raw materials, the whole process has low energy consumption and small emission.|[0017] 3. According to the coal chemical industry solid waste gas waste comprehensive utilization system, the adopted desulfurization and denitrification tower and the subsequent powder pretreatment module can realize the on-site treatment of all solid wastes, and further can realize the mixing of desulfurization ash and carbide slag, so that the crushing process is accelerated, the grinding time is saved, and the grinding efficiency is higher; and the final product is a solid block building material with usable strength, and after the system and the treatment process are introduced, the solid waste and the gas waste in the field of coal chemical industry can be directly treated into the product at one time without introducing additional auxiliary raw materials.|DRAWINGS DESCRIPTION|[0018] Fig. 1 is a schematic view of a flow and a structure of the comprehensive utilization system in the present application.|[0019] Fig. 2 is a schematic structural diagram of a mineralization reactor of the comprehensive utilization system in the present application.|[0020] In the figure:|[0021] 1-flue gas dust removal module, 2-carbon capture module, 3-desorption module, 4-desulfurization and denitration module, 5-solid waste raw material pretreatment module, 6-grinding briquetting module, 7-mineralization reaction module, 8-moving part, 9-air inlet, 10-air outlet, 11-dust removal cloth bag, 12-output shaft, 13-blowing pipe, 14-dust discharge port, 15-carbon capture absorption tower, 16-liquid storage tank, 17-circulation storage tank, 18-reflux tank, 19-carbon capture desorption tower, 20-air storage tank, 21-desulfurization and denitration tower, 22-exhaust port, 23-ash feed port, 24-storage tank, 25-weighing scale, 26-briquetting box, 27-briquetting plate, 28-rotating push rod, 29-ash discharge port, 30-handle, 31-base, 32-briquetting plate, 28-ash feed port and 33-autoclave.|INVENTION MODE|Detailed Description|[0022] The present invention will be described in detail with reference to the following examples. It is necessary to point out here that the following examples are only used for further illustration of the present invention, and should not be interpreted as a limitation of the scope of the present invention, and that the person skilled in the art would still belong to the scope of the present invention by some non-essential modifications and adjustments made by the above-mentioned contents of the present invention.|[0023] Example 1|[0024] As shown in fig. 1 and 2, the system module of the comprehensive utilization system for solid waste gas in coal chemical industry comprises a flue gas dust removal module 1, a carbon capture module 2, a desorption module 3, a desulfurization and denitrification module 4, a solid waste raw material pretreatment module 5, a grinding briquetting module 6 and a mineralization reaction module 7.|[0025] The flue gas dust removal module 1 is a cloth bag dust removal device; the bag-type dust collector comprises a moving part 8, an air inlet 9, an air outlet 10, a dust collecting bag 11 and a dust outlet 14; the moving part 8 is fixed on one side of the top of the bag-type dust collector, and the moving part 8 comprises a moving wheel and an output shaft 12 extending towards the interior of the box body of the moving part 8; 3-6 blowing pipes 13 are also fixed on the output shaft 12, and the blowing pipes 13 are mechanically and fixedly connected with the output shaft 12 through fixing pins; the gas inlet 9 is positioned in the middle of the box body of the bag-type dust collector and used for the entry of flue gas, and the gas outlet 10 is positioned at the top of the box body of the bag-type dust collector and used for the discharge of the flue gas after dust removal; the dust discharge port 14 is located at the bottom of the box body of the cloth bag dust removal device and used for discharging dust, and then collecting the dust.|[0026] The carbon capture module 2 is a carbon capture absorption device; the desorption module 3 is a carbon capture desorption device; the carbon capturing and absorbing device includes a carbon capturing and absorbing tower 15; a liquid storage tank 16 is also arranged at the bottom of the carbon capture absorption tower 15, and the liquid storage tank 16 is fixedly connected with a pipeline of an air outlet 10 of the cloth bag dust removal device; the carbon capture absorption device is also provided with a circulating storage tank 17 for carbon capture liquid; the circulating storage tank 17 is fixedly connected with the bottom end and the top of the carbon capture absorption tower 15 through pipelines, and a liquid inlet pump is arranged in a fixed pipeline connected with the top of the circulating storage tank and used for conveying the carbon capture liquid to the top of the carbon capture absorption tower 15; the carbon capture liquid is returned to the recycle storage tank 17 through an outlet at the bottom end after use.|[0027] The carbon capture desorption device comprises a carbon capture desorption tower 19, a gas storage tank 20 and a reflux groove 18; the top of the carbon capturing and desorbing tower 19 and the reflux groove 18 at the bottom end are fixedly connected with the circulating storage tank 17 through pipelines, and the carbon capturing and desorbing tower 19 and the gas storage tank 20 are fixedly connected through pipelines.|[0028] The desulfurization and denitrification module 4 is a desulfurization and denitrification tower 21; the bottom of the desulfurization and denitrification tower 21 is fixedly connected with a top end pipeline of the carbon capture absorption tower 15, and an exhaust port 22 is arranged at the top end of the desulfurization and denitrification tower 21 and used for discharging the desulfurized and denitrified flue gas; 11 carbide slag layers are arranged in the desulfurization and denitrification tower 21.|[0029] The solid waste raw material pretreatment module 5 comprises a powder weighing device; the powder weighing device is used for measuring and weighing the waste carbide slag and the desulfurization ash slag left in the desulfurization and denitrification tower 21; the solid waste raw material pretreatment module 5 also comprises a crushing device for primarily crushing the weighed ash.|[0030] The powder weighing device comprises an ash inlet 23, a storage box 24, a handle 30, an ash outlet 29, a base 31 and a weighing meter 25; the handle 30 and the ash discharging port 29 are respectively arranged at two opposite sides of the storage box 24, and the ash feeding port 23 is arranged at the top end of the storage box 24 and used for feeding and mixing carbide slag and desulfurization ash; the storage box 24 is detachably and fixedly connected to the top end of the base 31, and the base 31 comprises a weighing meter 25 for displaying the ash and slag quality value.|[0031] The abrasive compact module 6 includes a compact press; the briquetting machine comprises a briquetting box body 26, and a feed inlet 32 is formed in the top end of the briquetting box body 26 and used for feeding mixed ash; a rotary push rod 28 is arranged at the left end of the briquetting box body 26 and is used for driving the briquetting plate 27 on the same side in the briquetting box body 26 to extrude towards the other side; the grinding and briquetting module 6 also comprises a grinding device for grinding the briquetted workpieces.|[0032] The mineralization reaction module 7 is a mineralization reaction kettle; the mineralization reaction kettle is a continuous mineralization reaction kettle formed by connecting autoclaves 33 in parallel, and the number of the autoclaves 33 is 5.|[0033] For the convenience of understanding the technical solution of the present invention, the following detailed description is made on the working principle or the operation mode of the present invention in the practical process.|[0034] In the actual use process: the flue gas enters the system from the gas inlet of the bag-type dust collector, dust particles are removed through a dust removing bag to obtain corresponding impurity-removed flue gas, and then the corresponding impurity-removed flue gas flows out of the gas outlet, wherein the dust removing bag is cleaned through a blowing pipe in the device, and the moving part is used for adjusting the position of the blowing pipe through a control output shaft; the flowing impurity-removed flue gas enters a carbon capturing tower, at the moment, the carbon capturing liquid in the circulating storage tank is conveyed to the top of the carbon capturing tower to form convection with the upstream flue gas, so that carbon dioxide in the flue gas is captured and absorbed, and then the absorbed liquid flows back to the storage tank; enabling the flue gas subjected to carbon capture to enter a desulfurization and denitrification tower, performing desulfurization and denitrification through a calcium carbide layer, and then discharging the flue gas through an exhaust port; the carbon capture liquid in the circulating storage tank is conveyed to a carbon capture desorption tower to realize the desorption of carbon dioxide and is stored in a gas storage tank for standby; and then, conveying the desulfurized slag and the carbide slag used by the desulfurization and denitrification tower to a weighing device for mixing and primary crushing, weighing, conveying the mixed powder to a briquetting machine for mixing and briquetting with a small amount of cement to prepare a pressed piece, then conveying the pressed piece into a mineralization reaction kettle, and realizing mineralization reaction through the supply of carbon dioxide in a gas storage tank.|[0035] The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in other forms, and any person skilled in the art may modify or change the technical content disclosed above to equivalent embodiments with equivalent changes, but all those skilled in the art do not depart from the technical scope of the present invention, and any simple modifications made to the above embodiments according to the technical essence of the present invention, equivalent changes and modifications still belong to the protection scope of the technical solution of the present invention. (CN217549273)|TECHNICAL FIELD|[0001] The utility model belongs to the categorised B01D53/00 field of patent IPC, more specifically relates to a useless comprehensive utilization system of coal industry solid waste gas.|BACKGROUND ART|[0002] The coal chemical industry solid waste comprises gasified fly ash, gasified slag, coal slime, coal gangue, fly ash and the like, compounds containing silicon, aluminum, magnesium, iron and calcium, and a small amount of titanium, potassium, sodium, phosphorus and the like. In recent years, the utilization of industrial waste residues as raw materials of brickworks is a research hotspot in the field of solid waste treatment, so that the utilization rate of solid waste can be improved, the use of raw materials adopted by buildings can be saved, and the effects of energy conservation and emission reduction are achieved. The carbide slag is industrial waste slag formed after acetylene gas is produced by using carbide, and causes pollution to the environment. The carbide slag has fine particle size and high reaction activity, is mainly used for replacing limestone to prepare building and construction materials such as cement and the like by traditional large-scale consumption, but is limited by saturation of domestic markets, centralized geographic positions and the like; the main component of the carbide slag is calcium hydroxide which can be used for preparing chemical products such as calcium oxide, calcium carbonate and the like, but the treatment process is high in cost and easy to cause secondary pollution due to the influence of impurities in the carbide slag; the carbide slag is strongly alkaline, has better ablation property, has excellent performance in the environmental treatment processes of acid wastewater, flue gas desulfurization and the like, replaces a calcium-based absorbent for flue gas desulfurization, and becomes one of the development directions of comprehensive utilization of the carbide slag.|[0003] Therefore, the utility model provides a pair of make full use of in the coal chemical industry solid useless and useless comprehensive utilization system of gas to solve waste pollution and the problem that the utilization of the solid gas of coal chemical industry received the restriction.|DISCLOSURE|SUMMERY OF THE UTILITY MODEL|[0004] In order to solve the problems, the invention provides a coal chemical industry solid waste gas and waste gas comprehensive utilization system, and the system modules comprise a flue gas dust removal module 1, a carbon capture module 2, a desorption module 3, a desulfurization and denitrification module 4, a solid waste raw material pretreatment module 5, a grinding and briquetting module 6 and a mineralization reaction module 7.|[0005] As a preferred scheme, the flue gas dust removal module 1 is a cloth bag dust removal device; the cloth bag dust removal device comprises a moving part 8, an air inlet 9, an air outlet 10, a dust removal cloth bag 11 and a dust discharge hole 14; the moving part 8 is fixed on one side of the top of the bag-type dust collector, and the moving part 8 comprises moving wheels and an output shaft 12 extending towards the interior of the box body of the moving part 8; 3-6 blowing pipes 13 are further fixed on the output shaft 12, and the blowing pipes 13 are mechanically and fixedly connected with the output shaft 12 through fixing pins; the gas inlet 9 is positioned in the middle of the box body of the bag-type dust collector and used for allowing the flue gas to enter, and the gas outlet 10 is positioned at the top of the box body of the bag-type dust collector and used for discharging the flue gas after dust removal; the dust discharge hole 14 is located at the bottom of a box body of the cloth bag dust removal device and used for discharging dust, and then collecting the dust.|[0006] As a preferable mode, the carbon capture module 2 is a carbon capture absorption device; the desorption module 3 is a carbon capture desorption device; the carbon capture absorption device includes a carbon capture absorption tower 15; a liquid storage tank 16 is also arranged at the bottom of the carbon capture absorption tower 15, and the liquid storage tank 16 is fixedly connected with a pipeline of an air outlet 10 of the cloth bag dust removal device; the carbon capture and absorption device is also provided with a circulating storage tank 17 for carbon capture liquid; the circulating storage tank 17 is fixedly connected with the bottom end and the top of the carbon capture absorption tower 15 through pipelines, and a liquid inlet pump is arranged in a fixed pipeline connected with the top of the circulating storage tank and used for conveying the carbon capture liquid to the top of the carbon capture absorption tower 15; the carbon capture liquid is returned to the recycle storage tank 17 through an outlet at the bottom end after use.|[0007] As a preferable scheme, the carbon capture and desorption device comprises a carbon capture and desorption tower 19, a gas storage tank 20 and a reflux groove 18; the top of the carbon capture desorption tower 19 and the reflux groove 18 at the bottom are fixedly connected with the circulating storage tank 17 through pipelines, and the carbon capture desorption tower 19 and the gas storage tank 20 are fixedly connected through pipelines.|[0008] As a preferable scheme, the desulfurization and denitrification module 4 is a desulfurization and denitrification tower 21; the bottom of the desulfurization and denitrification tower 21 is fixedly connected with a top end pipeline of the carbon capture absorption tower 15, and an exhaust port 22 is arranged at the top end of the desulfurization and denitrification tower 21 and used for discharging desulfurized and denitrated flue gas; 5-20 carbide slag layers are arranged in the desulfurization and denitrification tower 21.|[0009] As a preferable scheme, the solid waste raw material pretreatment module 5 comprises a powder weighing device; the powder weighing device is used for measuring and weighing the waste carbide slag and the desulfurization ash slag left in the desulfurization and denitrification tower 21; the solid waste raw material pretreatment module 5 also comprises a crushing device for primarily crushing the weighed ash.|[0010] As a preferable scheme, the powder weighing device comprises an ash inlet 23, a storage box 24, a handle 30, an ash outlet 29, a base 31 and a weighing meter 25; the handle 30 and the ash discharging port 29 are respectively arranged at two opposite sides of the storage box 24, and the ash feeding port 23 is arranged at the top end of the storage box 24 and used for feeding and mixing carbide slag and desulfurization ash; the storage box 24 is detachably and fixedly connected to the top end of a base 31, and the base 31 comprises a weighing meter 25 for displaying the ash and slag mass value.|[0011] As a preferred solution, the abrasive compact module 6 comprises a compact press; the briquetting machine comprises a briquetting box 26, and a feed inlet 32 is formed in the top end of the briquetting box 26 and used for feeding mixed ash; a rotary push rod 28 is arranged at the left end of the briquetting box body 26 and is used for driving the briquetting plate 27 on the same side in the briquetting box body 26 to extrude towards the other side; the grinding and briquetting module 6 also comprises a grinding device for grinding the briquetted workpieces.|[0012] As a preferred scheme, the mineralization reaction module 7 is a mineralization reaction kettle; the mineralization reaction kettle is a continuous mineralization reaction kettle which is formed by connecting autoclaves 33 in series and/or in parallel.|[0013] In a preferred embodiment, the number of the autoclaves 33 is 5 to 20.|[0014] Has the advantages that:|[0015] 1. the utility model provides a useless comprehensive utilization system of solid waste gas of coal chemical industry can be through the synergism of a plurality of modules to realize the reutilization of the solid waste gas waste material in coal chemical industry field, and can realize the useless pair of processing of solid useless gas in the use of system, thereby improve system efficiency.|[0016] 2. The application provides a comprehensive utilization system for solid waste gas and waste gas in coal chemical industry,the adopted solid waste and gas waste raw materials can be obtained from local materials in chemical plants and the like, the solid waste is simply treated and directly pressed into building materials, and the trapped high-concentration CO is 2 Reacts with the massive building materials to obtain the building materials with the strength meeting the building requirements, thereby really realizing CO 2 The net emission reduction and the direct production of the product building materials from the coal chemical industry plant, but not the building material raw materials, the whole process has low energy consumption and small emission.|[0017] 3. According to the coal chemical industry solid waste gas waste comprehensive utilization system, the adopted desulfurization and denitrification tower and the subsequent powder pretreatment module can realize the on-site treatment of all solid wastes, and further can realize the mixing of desulfurization ash and carbide slag, so that the crushing process is accelerated, the grinding time is saved, and the grinding efficiency is higher; and the final product is a solid block building material with usable strength, and after the system and the treatment process are introduced, the solid waste and the gas waste in the field of coal chemical industry can be directly treated into the product at one time without introducing additional auxiliary raw materials.|DRAWINGS DESCRIPTION|[0018] Fig. 1 is a schematic view of a flow and a structure of the comprehensive utilization system in the present application.|[0019] Fig. 2 is a schematic structural diagram of a mineralization reactor of the comprehensive utilization system in the present application.|[0020] In the figure:|[0021] 1-flue gas dust removal module, 2-carbon capture module, 3-desorption module, 4-desulfurization and denitration module, 5-solid waste raw material pretreatment module, 6-grinding briquetting module, 7-mineralization reaction module, 8-moving part, 9-air inlet, 10-air outlet, 11-dust removal cloth bag, 12-output shaft, 13-blowing pipe, 14-dust discharge port, 15-carbon capture absorption tower, 16-liquid storage tank, 17-circulation storage tank, 18-reflux tank, 19-carbon capture desorption tower, 20-air storage tank, 21-desulfurization and denitration tower, 22-exhaust port, 23-ash feed port, 24-storage tank, 25-weighing scale, 26-briquetting box, 27-briquetting plate, 28-rotating push rod, 29-ash discharge port, 30-handle, 31-base, 32-briquetting plate, 28-ash feed port and 33-autoclave.|INVENTION MODE|Detailed Description|[0022] The present invention will be described in detail with reference to the following examples. It is necessary to point out here that the following examples are only used for further illustration of the present invention, and should not be interpreted as a limitation of the scope of the present invention, and that the person skilled in the art would still belong to the scope of the present invention by some non-essential modifications and adjustments made by the above-mentioned contents of the present invention.|[0023] Example 1|[0024] As shown in fig. 1 and 2, the system module of the comprehensive utilization system for solid waste gas in coal chemical industry comprises a flue gas dust removal module 1, a carbon capture module 2, a desorption module 3, a desulfurization and denitrification module 4, a solid waste raw material pretreatment module 5, a grinding briquetting module 6 and a mineralization reaction module 7.|[0025] The flue gas dust removal module 1 is a cloth bag dust removal device; the bag-type dust collector comprises a moving part 8, an air inlet 9, an air outlet 10, a dust collecting bag 11 and a dust outlet 14; the moving part 8 is fixed on one side of the top of the bag-type dust collector, and the moving part 8 comprises a moving wheel and an output shaft 12 extending towards the interior of the box body of the moving part 8; 3-6 blowing pipes 13 are also fixed on the output shaft 12, and the blowing pipes 13 are mechanically and fixedly connected with the output shaft 12 through fixing pins; the gas inlet 9 is positioned in the middle of the box body of the bag-type dust collector and used for the entry of flue gas, and the gas outlet 10 is positioned at the top of the box body of the bag-type dust collector and used for the discharge of the flue gas after dust removal; the dust discharge port 14 is located at the bottom of the box body of the cloth bag dust removal device and used for discharging dust, and then collecting the dust.|[0026] The carbon capture module 2 is a carbon capture absorption device; the desorption module 3 is a carbon capture desorption device; the carbon capturing and absorbing device includes a carbon capturing and absorbing tower 15; a liquid storage tank 16 is also arranged at the bottom of the carbon capture absorption tower 15, and the liquid storage tank 16 is fixedly connected with a pipeline of an air outlet 10 of the cloth bag dust removal device; the carbon capture absorption device is also provided with a circulating storage tank 17 for carbon capture liquid; the circulating storage tank 17 is fixedly connected with the bottom end and the top of the carbon capture absorption tower 15 through pipelines, and a liquid inlet pump is arranged in a fixed pipeline connected with the top of the circulating storage tank and used for conveying the carbon capture liquid to the top of the carbon capture absorption tower 15; the carbon capture liquid is returned to the recycle storage tank 17 through an outlet at the bottom end after use.|[0027] The carbon capture desorption device comprises a carbon capture desorption tower 19, a gas storage tank 20 and a reflux groove 18; the top of the carbon capturing and desorbing tower 19 and the reflux groove 18 at the bottom end are fixedly connected with the circulating storage tank 17 through pipelines, and the carbon capturing and desorbing tower 19 and the gas storage tank 20 are fixedly connected through pipelines.|[0028] The desulfurization and denitrification module 4 is a desulfurization and denitrification tower 21; the bottom of the desulfurization and denitrification tower 21 is fixedly connected with a top end pipeline of the carbon capture absorption tower 15, and an exhaust port 22 is arranged at the top end of the desulfurization and denitrification tower 21 and used for discharging the desulfurized and denitrified flue gas; 11 carbide slag layers are arranged in the desulfurization and denitrification tower 21.|[0029] The solid waste raw material pretreatment module 5 comprises a powder weighing device; the powder weighing device is used for measuring and weighing the waste carbide slag and the desulfurization ash slag left in the desulfurization and denitrification tower 21; the solid waste raw material pretreatment module 5 also comprises a crushing device for primarily crushing the weighed ash.|[0030] The powder weighing device comprises an ash inlet 23, a storage box 24, a handle 30, an ash outlet 29, a base 31 and a weighing meter 25; the handle 30 and the ash discharging port 29 are respectively arranged at two opposite sides of the storage box 24, and the ash feeding port 23 is arranged at the top end of the storage box 24 and used for feeding and mixing carbide slag and desulfurization ash; the storage box 24 is detachably and fixedly connected to the top end of the base 31, and the base 31 comprises a weighing meter 25 for displaying the ash and slag quality value.|[0031] The abrasive compact module 6 includes a compact press; the briquetting machine comprises a briquetting box body 26, and a feed inlet 32 is formed in the top end of the briquetting box body 26 and used for feeding mixed ash; a rotary push rod 28 is arranged at the left end of the briquetting box body 26 and is used for driving the briquetting plate 27 on the same side in the briquetting box body 26 to extrude towards the other side; the grinding and briquetting module 6 also comprises a grinding device for grinding the briquetted workpieces.|[0032] The mineralization reaction module 7 is a mineralization reaction kettle; the mineralization reaction kettle is a continuous mineralization reaction kettle formed by connecting autoclaves 33 in parallel, and the number of the autoclaves 33 is 5.|[0033] For the convenience of understanding the technical solution of the present invention, the following detailed description is made on the working principle or the operation mode of the present invention in the practical process.|[0034] In the actual use process: the flue gas enters the system from the gas inlet of the bag-type dust collector, dust particles are removed through a dust removing bag to obtain corresponding impurity-removed flue gas, and then the corresponding impurity-removed flue gas flows out of the gas outlet, wherein the dust removing bag is cleaned through a blowing pipe in the device, and the moving part is used for adjusting the position of the blowing pipe through a control output shaft; the flowing impurity-removed flue gas enters a carbon capturing tower, at the moment, the carbon capturing liquid in the circulating storage tank is conveyed to the top of the carbon capturing tower to form convection with the upstream flue gas, so that carbon dioxide in the flue gas is captured and absorbed, and then the absorbed liquid flows back to the storage tank; enabling the flue gas subjected to carbon capture to enter a desulfurization and denitrification tower, performing desulfurization and denitrification through a calcium carbide layer, and then discharging the flue gas through an exhaust port; the carbon capture liquid in the circulating storage tank is conveyed to a carbon capture desorption tower to realize the desorption of carbon dioxide and is stored in a gas storage tank for standby; and then, conveying the desulfurized slag and the carbide slag used by the desulfurization and denitrification tower to a weighing device for mixing and primary crushing, weighing, conveying the mixed powder to a briquetting machine for mixing and briquetting with a small amount of cement to prepare a pressed piece, then conveying the pressed piece into a mineralization reaction kettle, and realizing mineralization reaction through the supply of carbon dioxide in a gas storage tank.|[0035] The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in other forms, and any person skilled in the art may modify or change the technical content disclosed above to equivalent embodiments with equivalent changes, but all those skilled in the art do not depart from the technical scope of the present invention, and any simple modifications made to the above embodiments according to the technical essence of the present invention, equivalent changes and modifications still belong to the protection scope of the technical solution of the present invention. Family Number|(102093066)|102093066|Abstract|(CN217549273U U)|The utility model provides a coal chemical solid waste gas and waste comprehensive utilization system . The system module comprises a flue gas dust removal module , a carbon capture module , a desorption module , a desulfurization and denitrification module , a solid waste raw material pretreatment module , a grinding and briquetting module and a mineralization reaction module which are sequentially and fixedly connected through pipelines . Flue gas enters the system from a gas inlet of the bag - type dust removal device , dust particles are subjected to dust removal through a dust removal bag to obtain corresponding impurity - removed flue gas , the impurity - removed flue gas flows out from a gas outlet , the impurity - removed flue gas enters a carbon removal capture tower , carbon dioxide in the flue gas is captured and absorbed , and then absorption liquid flows back to a storage tank ; the flue gas after carbon capture enters a desulfurization and denitrification tower , is desulfurized and denitrified through a calcium carbide layer , and then is discharged from an exhaust port , desulfurization slag and carbide slag used by the desulfurization and denitrification tower are conveyed to a weighing device to be mixed , preliminarily crushed and weighed , and then mixed powder is conveyed to a briquetting machine to be mixed with a small amount of cement to be subjected to briquetting so as to prepare a pressed part . |IPC codes|(CN217549273U U)|B01D - 046/02 | Environmental technology B01D-046/02 B01D-046/02 CN118988936 CN118988936 112294671 WHO=Examiner SELF=N CAT=A GRANTED (CN217549273)|GRANTED ALIVE (CN217549273)|ALIVE (CN217549273)|LEGAL DETAILS FOR CN217549273|Actual or expected expiration date=2032-01-28|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-01-28|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202220240693|Application date=2022-01-28|Standardized application number=2022CN-U240693|Event publication date=2022-10-11|Event code=CN/U|Event indicator=Pos|Event group=Event indicating In Force|Registered Utility Model|Publication country=CN|Publication number=CN217549273|Publication stage code=U|Publication date=2022-10-11|Standardized publication number=CN217549273U|Event publication date=2022-10-11|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN217549273)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=jf59U3ybGzbb70iKaegSNqqLeopS8oZMbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000064943746&ekey=2408&xpn=CN217549273U&kind=U https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=7%252FZkFzHtYyxgf9IDWr1PfLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN217549273)|CN (CN217549273)|NAME=JIANGSU JICUI FUNCTIONAL MATERIALS RESEARCH INSTITUTE CO., LTD. , COUNTRY=CN (CN217549273)|NAME=CHENG MINGZHAO|NAME=LI YI|NAME=REN TIANBIN|NAME=JING ZHENZI|NAME=LI CHEN 0 1 Titre: (CN217549273)|Coal chemical solid waste gas and waste comprehensive utilization system Résumé: (CN217549273)|The utility model provides a coal chemical solid waste gas and waste comprehensive utilization system. The system module comprises a flue gas dust removal module, a carbon capture module, a desorption module, a desulfurization and denitrification module, a solid waste raw material pretreatment module, a grinding and briquetting module and a mineralization reaction module which are sequentially and fixedly connected through pipelines. Flue gas enters the system from a gas inlet of the bag-type dust removal device, dust particles are subjected to dust removal through a dust removal bag to obtain corresponding impurity-removed flue gas, the impurity-removed flue gas flows out from a gas outlet, the impurity-removed flue gas enters a carbon removal capture tower, carbon dioxide in the flue gas is captured and absorbed, and then absorption liquid flows back to a storage tank; the flue gas after carbon capture enters a desulfurization and denitrification tower, is desulfurized and denitrified through a calcium carbide layer, and then is discharged from an exhaust port, desulfurization slag and carbide slag used by the desulfurization and denitrification tower are conveyed to a weighing device to be mixed, preliminarily crushed and weighed, and then mixed powder is conveyed to a briquetting machine to be mixed with a small amount of cement to be subjected to briquetting so as to prepare a pressed part. 110 Abstract gpt-4o-mini no The article focuses on a system for carbon capture and flue gas treatment, which does not align with the topic of enhanced weathering or accelerated mineral alteration for CO₂ sequestration.
115 KR20230040905 KR10-2023-0040905 KR10-2680805 110482428 KR10-2680805 B1 2024-07-03 [KR102680805] 2023-03-29 2023-03-29 2024-07-03 (KR102680805)|2024-07-03 (KR10-2680805)|2043-03-29 (KR10-2680805)|Method for manufacturing soda lime for carbon dioxide absorption (KR10-2680805)|The present invention relates to a method for manufacturing soda lime for carbon dioxide absorption, having an excellent carbon dioxide removal rate even without an artificial specific surface area enhancement process through a separate crushing process and also preventing cracks or the like occurring during use by using an additive for enhancing specific surface area and an additive for improving strength. Provided is a method for manufacturing soda lime pellets with a spherical, a granular, or a columnar shape with an improved specific surface area of a millimeter level by using a disk pelletizing device, an extrusion pelletizing device, or a mixing pelletizing device. The soda lime pellets manufactured by the method according to the present invention have the advantage of being immediately usable without an additional grinding process.COPYRIGHT KIPO 2025 KOREA INSTITUTE OF LIMESTONE & ADVANCED MATERIALS (KR10-2680805)|KOREA INSTITUTE OF LIMESTONE AND ADVANCED MATERIALS ([KR]) CHO JIN SANG|KIM YOUNG JIN|KWON SEOK JE|SEO JUN HYUNG|KIM YANG SOO (KR10-2680805)|CHO JIN SANG|KIM YOUNG JIN|KWON SEOK JE|SEO JUN HYUNG|KIM YANG SOO (KR10-2680805)|KIM, JUNG-HYUN (KR10-2680805)|In addition, in order to prevent dust from being generated due to being destroyed during use, the soda lime powder should be manufactured with a certain strength or more, which makes grinding more difficult, thereby causing a problem in that the production yield of soda lime is lowered and production costs are increased.|However, the prior art does not specifically disclose a method for preparing a form of soda lime, which is an important factor for determining carbon dioxide absorption performance.|If the conditions are not satisfied, it may be difficult to achieve the desired size of the pellets due to difficulty in agglomeration, which may take more time to reach the desired size of the pellets, or it may be difficult to adjust the size of the pellets due to excessive agglomeration.|Sodalime used for medical purposes is practically unused or used in a very small amount because lithium is expensive compared to sodium and potassium hydroxides.| (KR10-2680805)|1. A method of manufacturing a multi-layered carbon dioxide pellet, the method comprising: a first step of manufacturing a first alkaline aqueous solution including sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet, and having a pH of 13 or more; a second step of manufacturing a second alkaline aqueous solution having a pH of 13 or more, in which any one viscosity agent selected from the group consisting of sodium polyacrylate, gelatin, and agar as a viscosity agent, or two or more viscosity agents are dissolved in the first alkaline aqueous solution; a third step of manufacturing a slaked lime powder mixture manufactured by mixing any one additive or two or more additives selected from the group consisting of active carbon and expanding clay minerals such as Montmorillonite, Bentonite, and Vermiculite zeolite, as an additive for enhancing a non-surface of calcium hydroxide (Ca(OH)2) and a non-surface of calcium hydroxide (CO., CO., LTD.); and a fourth step of mixing the second alkaline aqueous solution and the slaked lime powder mixture and manufacturing a multi-layered carbon dioxide pellet, thereby absorbing the non-layered carbon dioxide pellet A method of preparing soda lime for absorbing carbon dioxide, the method comprising: 4 to 10 m2/g; 15 to 32% calcium carbonate conversion; and 0.9 to 1.8% friability. |9. AMENDSTATUS: delete| (KR10-2680805)|The present invention provides a method for preparing a multi-layered carbon dioxide sorbent, the method comprising: a first step of preparing a first alkaline aqueous solution with a pH of 13 or higher, the first alkaline aqueous solution including sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet; a second step of preparing a second alkaline aqueous solution with a pH of 13 or higher, in which any one viscous agent selected from the group consisting of sodium polyacrylate, gelatin, and agar as a viscous agent, or two or more viscous agents are dissolved in the first alkaline aqueous solution; a third step of preparing a slaked lime powder mixture prepared by mixing any one additive or two or more additives selected from the group consisting of active carbon and expanding clay, such as Montmorillonite, Bentonite, vermiculite, and zeolite, as an additive for improving the non-surface; and a fourth step of mixing the first alkaline aqueous solution or the second alkaline aqueous solution with the slaked lime water to prepare a pellet-absorbing mixture for absorbing carbon dioxide gas.|The present invention relates to a manufacturing method of soda lime for absorbing carbon dioxide using domestic limestone resources.|To solve the above-described problems, the present invention provides a method for manufacturing soda-lime pellets, wherein the sodalime pellets have a specific surface area which is improved into several ㎜ of a spherical shape, granules, or pillars, by using an additive for improving a specific surface area and an additive for improving strength, without an artificial specific surface area improvement process through a separate grinding process, and can prevent cracks or the like which occur during use. Accordingly, it is an object of the present invention to provide a method for producing soda-lime pellets having a spherical shape, a granular shape or a columnar shape with an improved specific surface area using a disk pelletizing apparatus, an extrusion pelletizing apparatus or a mixing pelletizing apparatus.| (KR10-2680805)|SODA LIME(100,65)|CARBON DIOXIDE(100,51)|ABSORBING CARBON DIOXIDE(100,19)|CARBON DIOXIDE PELLET(100,3)|AMENDSTATUS(100,1)|DOMESTIC LIMESTONE RESOURCE(100,1)|MANUFACTURING SODA LIME(100,1)|SODALIME PELLET(99,3)|ALKALINE AQUEOUS SOLUTION(92,59)|VERMICULITE ZEOLITE(86,1)|EXTRUSION PELLETIZING(79,13)|GROW SPHERICAL SODALIME PELLET(74,1)|ADDITIVE(72,20)|DISC PELLETIZING(72,19)|GRANULAR SODALIME SEED(66,1)|LIMESTONE RESOURCE(66,1)|ENHANCING NONSURFACE(63,2)|SLAKED LIME(62,45)|MIXING PELLETIZING(62,13)|CALCIUM HYDROXIDE NONSURFACE(62,1)|SLAKED LIME POWDER MIXTURE(54,31)|SLAKED LIME DOUGH(53,8)|AGGLOMERATION(50,2)|PRODUCING SODA LIME PELLET(50,1)|SODA LIME PELLET(48,11)|MANUFACTURING SODA LIME PELLET(48,2)|ETHYL VIOLET(46,8)|SODA LIME MANUFACTURING(46,1)|SODA LIME POWDER(44,1)|MONTMORILLONITE(43,4)|ETHYL VIOLET EXPRESS(41,2)|CLAY MINERAL(40,4)|SPHERICAL SHAPE(35,5)|CYLINDRICAL DISC(34,14)|BENTONITE(33,6)|COLUMNAR SHAPE(33,3)|MIXING PELLETIZING MIXING BOWL(33,3)|ABSORPTION PERFORMANCE(33,1)|SLAKED LIME WATER(33,1)|CALCIUM CARBONATE CONVERSION(31,2)|POTASSIUM HYDROXIDE(30,7)|GELATIN(30,4)|CALCIUM HYDROXIDE(30,3)|GRANULAR SHAPE(30,3)|PELLET ABSORBING(30,1)|GRANULE(29,1)|GRANULAR SODA LIME SEED(28,7)|CARBON DIOXIDE SORBENT(28,2)|PILLAR(28,1)|CRACK(27,3)|AGAR(26,4)|CARBON DIOXIDE ABSORPTION PERFORMANCE(25,1)|FRIABILITY(24,9)|NAOH(24,5)|NONSURFACE(24,3)|SODIUM POLYACRYLATE(23,9)|VERMICULITE(23,3)|CRUSHING(23,2)|POWDER MIXTURE(22,31)|GRINDING(22,1)|CLAY(21,1)|PRODUCTION COST(21,1)|SODIUM HYDROXIDE(20,7)|ZEOLITE(20,2)|PRIMARY STIRRING(18,3)|LITHIUM(18,2)|TILT(17,1)|CALCIUM CARBONATE(16,17)|MEDIAN DIAMETER(16,8)|TABLET FRIABILITY(16,3)|PELLET DESIRED SIZE(15,2)|SPHERICAL SODA LIME PELLET(15,2)|STIRRING SPEED(14,6)|ACTIVE CARBON(14,4)|SHOW THERMOGRAVIMETRIC ANALYSIS(13,6)|GRANULAR SODA LIME COHESION(13,1)|PATIENT UNDERGOING ANESTHESIA SURGERY(13,1)|LIMESTONE FIRING FURNACE(12,1)|MIXER BOWL(11,3)|CARBON DIOXIDE ABSORPTION CAPACITY(11,2)|MIXER PADDLE(11,2)|MASSON FRIABILITY(10,1)|CARBON DIOXIDE REACTION(9,14)|MEDIAN LENGTH(8,4)|ADSORBENT PELLET(8,1)|AIRWAY DISEASE(8,1)|ARAGONITE(6,3)|CALCITE(6,3)|CALCIUM CARBONATE CRYSTAL(6,3)|CARBON DIOXIDE SORBENT PELLET(6,1)|COLUMNAR SHAPE GRANULE(6,1)|DISCHARGED SODA LIME(6,1)|FRIABILITY ANALYSIS(6,1)|MEETING MOISTURE(6,1)|OXYGEN BOMBE(6,1)|SODA LIME PARTICLE(6,1)|ABSORB CARBON DIOXIDE(5,2)|INGREDIENT COMPOSITION RATIO(5,2)|AUXILIARY TOOL(5,1)|COHESIVE STRENGTH(5,1)|DRYING FURNACE(5,1)|ETHYL VIOLET SOLUTION(5,1)|HYPERCARBONEMIA(5,1)|INCINERATOR EXHAUST GAS(5,1)|INDICATOR CARBONIC ACID(5,1)|INGREDIENT CONTENT(5,1)|REVOLUTION MOTION(5,1)|SODA LIME STRENGTH(5,1)|REDUCTION CHANGE(4,3)|AIR CIRCULATION(4,1)|BOILER(4,1)|CAPTURING CARBON DIOXIDE(4,1)|CARDIAC ARRHYTHMIA(4,1)|CONVERTING CALCIUM HYDROXIDE(4,1)|DECARBOXYLATION VALUE(4,1)|DROPLET(4,1)|DRYING LOSS(4,1)|EXPLOSION(4,1)|EXTRUDER(4,1)|FERMENTED SOYBEAN(4,1)|FINE POWDER(4,1)|FISHERIES INDUSTRY(4,1)|FRIABILITY SCHEMATIC DIAGRAM(4,1)| (KR10-2680805)|1. A method of manufacturing a multi-layered carbon dioxide pellet, the method comprising: a first step of manufacturing a first alkaline aqueous solution including sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet, and having a pH of 13 or more; a second step of manufacturing a second alkaline aqueous solution having a pH of 13 or more, in which any one viscosity agent selected from the group consisting of sodium polyacrylate, gelatin, and agar as a viscosity agent, or two or more viscosity agents are dissolved in the first alkaline aqueous solution; a third step of manufacturing a slaked lime powder mixture manufactured by mixing any one additive or two or more additives selected from the group consisting of active carbon and expanding clay minerals such as Montmorillonite, Bentonite, and Vermiculite zeolite, as an additive for enhancing a non-surface of calcium hydroxide (Ca(OH)2) and a non-surface of calcium hydroxide (CO., CO., LTD.); and a fourth step of mixing the second alkaline aqueous solution and the slaked lime powder mixture and manufacturing a multi-layered carbon dioxide pellet, thereby absorbing the non-layered carbon dioxide pellet A method of preparing soda lime for absorbing carbon dioxide, the method comprising: 4 to 10 m2/g; 15 to 32% calcium carbonate conversion; and 0.9 to 1.8% friability. |2. The method of claim 1, wherein the method comprises: a step 4-1 of tilting a cylindrical disk of a disk pelletizing apparatus, putting the slaked lime powder mixture into the cylindrical disk, rotating the same, and mixing the same; a step 4-2 of spraying the first alkaline aqueous solution or the second alkaline aqueous solution onto the slaked lime powder mixture mixed in the cylindrical disk to grow spherical sodalime pellets; and a step 4-3 of obtaining spherical sodalime pellets having a diameter of 2 to 4 ㎜. |3. The method of claim 2, wherein the slaked lime powder mixture rotates the cylindrical disk of the disk pelletizing apparatus at a tilt of 30 to 50° and a stirring speed of 20 to 30rpm. |4. The method of claim 2, wherein the second alkaline aqueous solution is sprayed at 5 to 9 ㎖/min. |5. The method of claim 1, wherein the sodalime pellet for absorbing carbon dioxide comprises: step 4-4 of mixing the slaked lime powder mixture and the first or second alkaline aqueous solution to prepare slaked lime dough for extrusion; step 4-5 of drying the slaked lime dough in an extrusion pelletizing apparatus to prepare cylindrical sodalime-pellets having an average diameter of 4 ㎜; and step 4-6 of drying and cutting the cylindrical sodalime-pellets to obtain cylindrical sodalime-pellets having an average diameter of 4 ㎜ and an average length of 10 ㎜. |6. The method of claim 1, wherein the sodalime pellets for absorbing carbon dioxide comprise: step 4-7 of adding the first alkaline aqueous solution or the second alkaline aqueous solution while primarily stirring the slaked lime powder mixture in a mixing bowl of a mixing pelletizing apparatus to prepare granular sodalime seeds; and step 4-8 of secondarily stirring the granular sodalime seeds to prepare granular sodalime-pellets. |7. The method of claim 6, wherein the primary stirring is performed at 52 to 72rpm. for 2 to 5 minutes, and the secondary stirring is performed at 110 to 140rpm. for 1 to 5 minutes. |8. The method of claim 1, wherein the ethyl violet expresses purple color when the pH value of the soda lime for absorbing carbon dioxide is lowered to 10 or less, thereby indicating that the absorption capacity of carbon dioxide of the soda lime for absorbing carbon dioxide is lowered. |9. AMENDSTATUS: delete (KR10-2680805)|TECHNICAL FIELD|[0001] The present invention relates to a manufacturing method of soda lime for absorbing carbon dioxide using domestic limestone resources.|BACKGROUND ART|[0003] A technology for capturing carbon dioxide mineralization using soda lime generated from limestone is used in various fields such as medical, leisure, food, environment, military and fisheries industries as well as environmental significance for realizing carbon neutrality. In the medical field, since carbon dioxide is removed from circulating air by being used in a respirator of a patient undergoing anesthesia surgery, the respirator is used to prevent poisoning or oxygen from being deficient, and is also used as an auxiliary tool for preventing hypercarbonemia, hypertension, tachycardia, skin dryness, cardiac arrhythmia, brain blood flow, and increase in brain pressure, which are caused by an excessively high concentration of carbon dioxide. In addition, the leisure industry is used to prevent the concentration of carbon dioxide in the body from increasing in the diving field where divers dive with oxygen bombes. In the food industry, carbon dioxide generated during the decomposition of sugar and protein under oxygen-free conditions by microorganisms is removed in industries such as liquor, kimchi, and fermented soybean, using a fermentation process, and thus the present invention can be used to prevent expansion, explosion, or damage of packaging materials due to carbon dioxide generated during the distribution process.|[0004] Korean Patent Application No. 10-2004-0013047 discloses a size, hardness, drying loss, and carbon dioxide absorption capacity of soda lime particles; Korean Patent Application No. 10-2008-010367 discloses a method for preparing a carbon dioxide adsorbent having a porous channel using X13 zeolite, lithium hydroxide, and soda lime; and Korean Patent Registration No. 10-2438061 discloses a method for using soda lime to react with carbon dioxide in an exhaust gas discharge part such as a boiler, a limestone firing furnace, a drying furnace, and an incinerator exhaust gas of a papermaking process and to separate and recover the same in the form of carbonate. However, the prior art does not specifically disclose a method for preparing a form of soda lime, which is an important factor for determining carbon dioxide absorption performance. In general, soda lime is used by preparing a bulk cured body and then grinding it to a certain size. In particular, when it is manufactured from a fine powder, the specific surface area increases, thereby improving the efficiency of carbon dioxide removal. However, when fine dust generated in the pulverization process and fine dust generated in cracks of particles are present, the fine dust is inhaled into the respiratory tract to cause inflammation or remain in food to deteriorate marketability, and thus it has to be removed through a complicated process. In addition, in order to prevent dust from being generated due to being destroyed during use, the soda lime powder should be manufactured with a certain strength or more, which makes grinding more difficult, thereby causing a problem in that the production yield of soda lime is lowered and production costs are increased. |[0005] The patent documents and references referred to herein are incorporated herein by reference to the same extent that each document is individually and clearly specified by reference. |CITATION LIST|PATENT LITERATURE|[0007] Korean Patent Application No. 10-2004-0013047|Korean Patent Application No. 10-2008-010367|Korean Patent Registration 10-2438061|SUMMARY OF INVENTION|TECH PROBLEM|[0008] To solve the above-described problems, the present invention provides a method for manufacturing soda-lime pellets, wherein the sodalime pellets have a specific surface area which is improved into several ㎜ of a spherical shape, granules, or pillars, by using an additive for improving a specific surface area and an additive for improving strength, without an artificial specific surface area improvement process through a separate grinding process, and can prevent cracks or the like which occur during use.|[0009] Accordingly, it is an object of the present invention to provide a method for producing soda-lime pellets having a spherical shape, a granular shape or a columnar shape with an improved specific surface area using a disk pelletizing apparatus, an extrusion pelletizing apparatus or a mixing pelletizing apparatus.|[0010] Other objects and technical features of the present invention will be more specifically presented by the following detailed description of the present invention, claims, and drawings. |TECH SOLUTION|[0012] The present invention provides a method for preparing a multi-layered carbon dioxide sorbent, the method comprising: a first step of preparing a first alkaline aqueous solution with a pH of 13 or higher, the first alkaline aqueous solution including sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet; a second step of preparing a second alkaline aqueous solution with a pH of 13 or higher, in which any one viscous agent selected from the group consisting of sodium polyacrylate, gelatin, and agar as a viscous agent, or two or more viscous agents are dissolved in the first alkaline aqueous solution; a third step of preparing a slaked lime powder mixture prepared by mixing any one additive or two or more additives selected from the group consisting of active carbon and expanding clay, such as Montmorillonite, Bentonite, vermiculite, and zeolite, as an additive for improving the non-surface; and a fourth step of mixing the first alkaline aqueous solution or the second alkaline aqueous solution with the slaked lime water to prepare a pellet-absorbing mixture for absorbing carbon dioxide gas.|[0013] The soda lime pellets for absorbing carbon dioxide are characterized by including: a 4-1 step of tilting the cylindrical disk of a disk pelletizing apparatus, putting the slaked lime powder mixture in the cylindrical disk, rotating the same, and mixing the same; a 4-2 step of spraying the first alkaline aqueous solution or the second alkaline aqueous solution into the slaked lime powder mixture mixed in the cylindrical disk to grow spherical soda lime pellets; and a 4-3 step of obtaining spherical soda lime pellets having a diameter of 2-4 ㎜.|[0014] The slaked lime powder mixture is characterized in that the cylindrical disk of the disk pelletizing apparatus is rotated under the conditions of a slope of 30 to 50° and a stirring speed of 20 to 30rpm, and the first alkaline aqueous solution or the second alkaline aqueous solution is sprayed at 5 to 9 ㎖/min.|[0015] The method of preparing soda lime-pellets for carbon dioxide absorption may include: step 4-4 of mixing the slaked lime powder mixture with the first alkaline aqueous solution or the second alkaline aqueous solution to prepare slaked lime dough for extrusion; step 4-5 of preparing cylindrical soda-lime-pellets having an average diameter of 4 ㎜ in an extrusion type pelletizing apparatus; and step 4-6 of drying and then cutting the cylindrical soda-lime-pellets to obtain pillar-shaped soda-lime-pellets having an average diameter of 4 ㎜ and an average length of 10 ㎜.|[0016] In addition, the method of preparing soda lime pellets for absorbing carbon dioxide includes: step 4-7 of preparing granular soda lime seeds by adding the first alkaline aqueous solution or the second alkaline aqueous solution while primarily stirring the slaked lime powder mixture in a mixing bowl of a mixing pelletizing apparatus; and step 4-8 of preparing granular soda lime-pellets by secondarily stirring the granular soda lime seeds.|[0017] The primary stirring may be performed at 52 to 72rpm. for 2 to 5 minutes, and the secondary stirring may be performed at 110 to 140rpm. for 1 to 5 minutes.|[0018] The ethyl violet expresses purple when the pH of the soda lime for absorbing carbon dioxide is lowered to 10 or less to indicate that the absorption capacity of the soda lime for absorbing carbon dioxide is lowered, and the soda lime for absorbing carbon dioxide has a specific surface area of 4 to 10 m2/g, a conversion rate of calcium carbonate of 15 to 32%, and friability of 0.9 to 1.8%.|ADVANTAGEOUS EFFECTS|[0020] The present invention uses an additive for improving a specific surface area and an additive for improving strength to not only have an excellent carbon dioxide removal rate without an artificial specific surface area improvement process through a separate crushing process but also prevent cracks or the like which are generated during use. In a manufacturing method, soda lime pellets having a ㎜ level of spherical shape, granular shape or columnar shape with an improved specific surface area are manufactured using a disk pelletizing apparatus, an extrusion pelletizing apparatus or a mixing pelletizing apparatus.|DESCRIPTION OF DRAWINGS|[0022] FIG. 1 shows a disk pelletizing apparatus of the present invention. FIG. 2 shows an extrusion pelletizing apparatus of the present invention. FIG. 3 shows the mixing pelletizing apparatus of the present invention. FIG. 4 shows thermogravimetric analysis and XRD analysis results of spherical soda-lime-pellet of the present invention. FIG. 5 shows thermogravimetric analysis and XRD analysis results for the pillar-shaped soda lime-pellet of the present invention. FIG. 6 shows thermogravimetric analysis and XRD analysis results for the granular soda-lime-pellet of the present invention. FIG. 7 shows a Tablet Friability Test method of the present invention.|DESCRIPTION OF EMBODIMENTS|[0023] The present invention provides a method for preparing a multi-layered carbon dioxide sorbent, the method comprising: a first step of preparing a first alkaline aqueous solution having a pH of 13 or higher, the first alkaline aqueous solution including sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet; a second step of preparing a second alkaline aqueous solution having a pH of 13 or higher, in which any one viscosity agent selected from the group consisting of sodium polyacrylate, gelatin, and agar as a viscosity agent, or two or more viscosity agents are dissolved in the first alkaline aqueous solution; a third step of preparing a slaked lime powder mixture prepared by mixing any one additive or two or more additives selected from the group consisting of montmorillonite, bentonite, vermiculite and active carbon, the additive serving as a non-surface enhancing additive, with the second alkaline aqueous solution; and a fourth step of mixing the slaked lime powder mixture with the second alkaline aqueous solution and pelletizing the mixture to prepare a multi-layered carbon dioxide sorbent pellet.|[0024] The soda lime of the present invention is manufactured by using lime as a main component and adding sodium hydroxide (NaOH), potassium hydroxide (KOH), and the like, and has a property of absorbing carbon dioxide in the atmosphere. A small amount of hydroxides such as sodium (Na), potassium (K), lithium (Li), and the like are added to the soda lime for absorbing carbon dioxide, and this serves as a catalyst for converting calcium hydroxide to calcium carbonate (CaCO3) by absorbing carbon dioxide. Sodalime used for medical purposes is practically unused or used in a very small amount because lithium is expensive compared to sodium and potassium hydroxides. |[0025] The reaction in which the soda lime absorbs carbon dioxide is the same as Chemical Formulas (1) and (2), and sodium hydroxide is repeatedly extinguished and regenerated until calcium hydroxide is all converted to calcium carbonate.|[0026] |[0027] |[0028] The soda lime for absorbing carbon dioxide of the present invention can be prepared in the form of pellets at a ㎜ level without any additional pulverization, and specifically, can be prepared by a disk pelletizing apparatus, an extrusion pelletizing apparatus, or a mixing pelletizing apparatus. |[0029] When a disk pelletizing apparatus is used, the method for manufacturing soda-lime pellets for absorbing carbon dioxide may be a manufacturing method, comprising: a step 4-1 of tilting the cylindrical disk of the disk pelletizing apparatus, and then inserting and rotating and mixing the slaked lime powder mixture; a step 4-2 of spraying the second alkaline aqueous solution to the slaked lime powder mixture mixed in the cylindrical disk so as to grow spherical soda-lime pellets; and a step 4-3 of obtaining spherical soda-lime pellets having a diameter of 2 to 4 ㎜. The slaked lime powder mixture is characterized in that the cylindrical disk of the disk pelletizing apparatus is rotated under the conditions of a slope of 30 to 50° and a stirring speed of 20 to 30rpm, and the second alkaline aqueous solution is sprayed at 5 to 9 ㎖/min. If the conditions are not satisfied, it may be difficult to achieve the desired size of the pellets due to difficulty in agglomeration, which may take more time to reach the desired size of the pellets, or it may be difficult to adjust the size of the pellets due to excessive agglomeration. |[0030] When an extrusion-type pelletizing apparatus is used, the method of manufacturing the soda lime pellets for absorbing carbon dioxide may include: step 4-4 of mixing the slaked lime powder mixture with the first alkaline aqueous solution or the second alkaline aqueous solution to prepare slaked lime dough for extrusion; step 4-5 of drying the slaked lime dough in an extrusion-type pelletizing apparatus to prepare cylindrical soda lime-pellets having an average diameter of 4 ㎜; and step 4-6 of drying and cutting the cylindrical soda lime-pellets to obtain cylindrical soda lime-pellets having an average diameter of 4 ㎜ and an average length of 10 ㎜. |[0031] When the mixing pelletizing apparatus is used, the method of preparing the soda lime pellets for absorbing carbon dioxide may include: step 4-7 of preparing granular soda lime seeds by adding the first alkaline aqueous solution or the second alkaline aqueous solution while primarily stirring the slaked lime powder mixture in the mixing bowl of the mixing pelletizing apparatus; and step 4-8 of preparing granular soda lime-pellets by secondarily stirring the granular soda lime seeds and increasing strength. The primary stirring may be performed at 52 to 72rpm. for 2 to 5 minutes, and the secondary stirring may be performed at 110 to 140rpm. for 1 to 5 minutes. If the above conditions are not satisfied, an appropriate granular soda-lime seed may not be formed, and thus, a pellet may not be prepared. |[0032] In the sodalime of the present invention, a small amount of an ethyl violet may be added so that the carbon dioxide absorption limit may be checked with the naked eye. At this time, the indicator forms carbonic acid along with moisture while the soda lime absorbs carbon dioxide, and accordingly, as the pH falls below 10, the color of the soda lime turns purple, which is an indicator of whether the soda lime loses its ability to absorb carbon dioxide. |[0033] The soda lime for absorbing carbon dioxide of the present invention has a specific surface area of 4 to 10 m2/g, a calcium carbonate conversion rate of 15 to 32%, and friability of 0.9 to 1.8%. |[0034] Hereinafter, the present invention will be described in detail with reference to Examples. |[0036] embodiment |[0038] 1. Methods of experiment; |[0039] 1) Preparation of Alkaline Aqueous Solution |[0040] In the present invention, soda lime was prepared by using an alkaline aqueous solution. The alkaline aqueous solution is mixed with Slaked lime (Ca(OH)2) and serves as a catalyst for reaction with carbon dioxide (CO2) and a limit indicator of the reaction. First, a first alkaline aqueous solution was prepared. A first alkaline aqueous solution was prepared by dissolving sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet (EV, Ethyl violet) in water at an appropriate ratio and a pH of 13 or higher. |[0041] The ethyl violet is used as a pH indicator of soda lime of the present invention. Soda lime absorbs carbon dioxide to form water and carbonic acid. As a result, the pH decreases to less than 10, which means that the soda lime lost its ability to absorb carbon dioxide. Conventional indicators monitor the pH change in the solution phase. In the present invention, since the soda lime is prepared by adding ethyl violet as an indicator, the soda lime absorbs carbon dioxide sufficiently and becomes purple when the pH is below 10, thereby indicating the loss of carbon dioxide removal ability. Since the ethyl violet does not have good solubility in water, when a solid sample is used, it should be diluted in an organic solvent including an OH group such as ethanol or methanol. Therefore, in the present invention, 0.1% ethyl violet diluted in methanol was used.|[0042] In order to increase the strength of the soda lime, a viscous agent was added to the first alkaline aqueous solution to prepare a second alkaline aqueous solution, and then reacted with lime. |[0043] As the viscosity agent, a material such as Sodium polyacrylate (SPA), gelatin, agar, or the like, which improves viscosity and increases stability of colloidal materials may be used, and preferably, Sodium polyacrylate (SPA) may be used. In the present invention, SPA was added in an amount of 0.1 to 0.3 parts by weight based on 100 parts by weight of the first alkaline aqueous solution and then mixed to prepare a second alkaline aqueous solution. The viscous material has the effect of increasing the strength of soda lime.|[0044] Table 1 below shows the composition of the first alkaline aqueous solution of the present invention, and Table 2 shows the composition of the second alkaline aqueous solution of the present invention.|[0045]  ingredientcomposition ratiofirst alkaline aqueous solutionsodium hydroxide 10 wt.% potassium hydroxide8 wt.% 0.1% ethyl violet solution12 wt.% water70 wt.%|TABLE 2|[0046]  ingredientcomposition ratiosecond alkaline aqueous solutionfirst alkaline aqueous solution100 parts by weight sodium polyacrylate0.1 to 0.3 parts by weight|[0048] 2) Preparation of Slaked Lime Powder Mixture |[0049] The second alkaline aqueous solution prepared above and the slaked lime powder mixture were mixed to prepare soda lime and pelletized in the preparation process. |[0050] In the slaked lime powder mixture of the present invention, a specific surface enhancing additive was used in order to increase the specific surface area of soda lime to improve reactivity with carbon dioxide. As the additive for enhancing non-surface, clay minerals or active carbon may be used. Since the clay mineral expands in volume by meeting moisture and contracts again during drying, the clay mineral has an effect of increasing the specific surface area of soda lime, and montmorillonite, bentonite, or vermiculite may be used. In the present invention, bentonite was used as the additive for enhancing the specific surface, and the additive for enhancing the specific surface may be used in a weight ratio of slaked lime: the additive for enhancing the specific surface=80 to 90: 20 to 10.|[0051] Table 3 below shows the composition of the slaked lime powder mixture of the present invention.|[0052]  ingredientcontentslaked lime powder mixtureslaked lime (Ca(OH)2)87.8 wt % bentonite12.2 wt %|[0053] In the present invention, a method of pelletizing by mixing the above raw materials was developed. The pelletizing method was manufactured in three types, such as a disk type, an extruder type, and a mixing type. Sodalime made in a certain shape was dried at 105°C for about 2 hours to secure strength, and the performance of the product was tested. |[0055] (1) Preparation of Soda Lime Using Disk Method |[0056] Spherical soda lime-pellet (Example 1) was prepared using a disk pelletizing apparatus (see FIG. 1). FIG. 1 shows a disk pelletizing apparatus of the present invention. Panel A) shows a disk pelletizing apparatus; panel B) schematically shows controlling the angle of the cylindrical disks of the disk pelletizing apparatus; panel C) schematically shows controlling the rotational speed of the cylindrical disks of the disk pelletizing apparatus and discharging spherical soda lime-pellets; and panel D) shows spherical soda lime-pellets prepared through the disk pelletizing apparatus. 410g (360g of slaked lime and 50 g of a non-surface enhancing additive) of a slaked lime powder mixture was put in a cylindrical disk (diameter of 400 ㎜) of a disk pelletizing apparatus, and the disk was rotated under conditions of a slope of 40° and a stirring speed of 25rpm. When the disk rotates, the slaked lime powder mixture rises along the surface of the disk and then flows down along the inclined surface by gravity. In this case, the first alkaline aqueous solution or the second alkaline aqueous solution was sprayed at 7 ㎖/min to prepare a soda-lime seed in which a droplet and a raw material were bonded. The soda lime seed is grown in a spherical shape while repeating the up-and-down motion along the rotating disk wall, and when it becomes a certain size and weight, it is discharged without further participating in the up-and-down motion. Among the discharged soda lime, small particles that are not used in the product can be recycled as soda lime seeds in the manufacturing process through sieving. In the present invention, a spherical sodalime-pellet having a diameter of 2 to 4 ㎜ was prepared by using the method.|[0058] (2) Preparation of Soda Lime by Extrusion |[0059] A columnar soda lime-pellet (Example 2) was prepared using an extrusion-type pelletizing apparatus (see FIG. 2). FIG. 2 shows an extrusion pelletizing apparatus of the present invention. Panel A) shows an extrusion pelletizing apparatus; and Panel B) shows columnar soda lime-pellets made using the extrusion pelletizing apparatus. First, the slaked lime powder mixture and the first alkaline aqueous solution or the second alkaline aqueous solution were mixed to prepare a slaked lime dough for extrusion. The first or second alkaline aqueous solution was put into a mixer bowl and stirred at a rotation speed of 62rpm for 5 minutes while adding a slaked lime powder mixture to prepare a slaked lime dough for extrusion. The slaked lime dough for extrusion was put into an extrusion-type pelletizing apparatus, and then, an inner screw feeder was rotated to slowly push it out to an extrusion unit, and a perforated plate having an average diameter of 4 ㎜ was mounted on the extrusion unit to prepare cylindrical soda lime-pellets having a diameter of 4 ㎜ (see FIG. 2). different perforated plates have different diameters to produce column-shaped sodalime-pellets of different diameters. The prepared pillar-shaped soda lime-pellets were dried at 105°C. for 2 hours or more and then cut to prepare pillar-shaped soda lime-pellets having an average diameter of 4㎜ and an average length of 10㎜.|[0061] (3) Preparation of Soda Lime Using Mixer Method |[0062] Granular soda-lime-pellet (Example 3) was prepared using a mixing pelletizing apparatus (see FIG. 3). FIG. 3 shows the mixing pelletizing apparatus of the present invention. Panel A) shows a mixing pelletizing apparatus; Panel B) shows granular soda lime-pellets prepared using the mixing pelletizing apparatus. First, the slaked lime powder mixture was put into a mixing bowl, and then a second alkaline aqueous solution was added while stirring the mixing paddle at a low speed (primary stirring) to prepare a granular soda-lime seed and then stirred at a high speed (secondary stirring) to prepare a granular soda-lime-pellet. |[0063] The mixing paddle performs rotation and revolution motions in the mixing bowl. The slaked lime powder mixture and the second alkaline aqueous solution are agglomerated while colliding with the mixer bowl wall and the mixer paddle to produce a granular soda-lime seed. The size of the granular soda-lime seed is determined according to the interval between the mixer paddle and the mixer bowl, and the cohesive strength of the granular soda-lime seed is determined according to the stirring speed. The granular soda-lime seed was sufficiently stirred to grow to a desired size, and after reaching the desired size, the stirring speed was increased to improve the cohesion of the granular soda-lime. |[0064] In the present invention, the interval between the mixer paddle and the mixer bowl was adjusted to 10 to 15 ㎜, and a slaked lime powder mixture and a second alkaline aqueous solution were added and stirred at low speed (62 rpm) for 2 to 5 minutes to prepare a granular soda-lime seed having a diameter of 10mm or less. Then, the mixture was stirred at high speed for 1 to 5 minutes (125 rpm) to prepare a granular soda lime.|[0066] 2. Results of experiments; |[0067] The spherical soda-lime-pellet (Example 1), the columnar soda-lime-pellet (Example 2), and the granular soda-lime-pellet (Example 3) were sieved to obtain a sample having a particle size of 2 to 4 ㎜. The sample was reacted for 20 minutes at a flow rate of 1L/min with 99% CO2 gas. The samples were subjected to Thermogravimetric Analysis (TGA), X-Ray Diffraction pattern (XRD), Brunauer-Emmett-Teller analysis (BET), and Masson Friability. The physical properties of the sample were measured before the reaction, and the calcium carbonate (CaCO3) conversion rate and strength were evaluated through the analysis after the reaction.|[0069] 1) Results of Thermogravimetric Analysis and X-ray Diffraction Analysis |[0070] As a result of thermogravimetric analysis on the soda lime of the present invention in which carbon dioxide was reacted, it was confirmed that the weight was reduced by the bound water at about 400°C in common. In the case of soda lime before the carbon dioxide reaction, the weight reduction characteristics were shown by the bound water, and in the case of soda lime after the carbon dioxide reaction, the weight reduction curve by the decarboxylation reaction of typical calcium carbonate was shown at about 600°C.|[0071] FIG. 4 shows thermogravimetric analysis and XRD analysis results of spherical soda-lime-pellet of the present invention. Panel A) shows the results of analyzing the reduction change before and after the carbon dioxide reaction; and Panel B shows the results of the XRD analysis before and after the carbon dioxide reaction. As a result of thermogravimetric analysis of spherical soda-lime-pellet, it was confirmed that a loss of about 24.12 wt. % occurred up to about 600 to 700°C. The above result is considered to be due to the fact that spherical soda lime-pellet absorbed carbon dioxide and became carbonated. The results are supported by the results of XRD analysis of spherical soda-lime-pellet. As a result of XRD analysis of spherical soda lime-pellet, it was confirmed that only lime crystals were found in the case of soda lime before the carbon dioxide reaction, but calcium carbonate crystals (Calcite, Aragonite) were grown in the case of soda lime after the carbon dioxide reaction. This means that the weight loss confirmed in the thermogravimetric analysis is due to calcium carbonate.|[0072] FIG. 5 shows thermogravimetric analysis and XRD analysis results for the columnar soda-lime-pellet (Example 2) of the present invention. Panel A) shows the results of analyzing the reduction change before and after the carbon dioxide reaction; and Panel B shows the results of the XRD analysis before and after the carbon dioxide reaction. As a result of thermogravimetric analysis on the columnar soda-lime-pellet, it was confirmed that a loss of about 13.72 wt.% occurred up to about 600 to 700°C. The above result is believed to be due to the fact that the columnar soda-lime-pellet absorbed carbon dioxide and became carbonated. The above result is supported by the XRD analysis result of columnar soda-lime-pellet. As a result of XRD analysis of the columnar soda lime-pellet, it was confirmed that only lime crystals were found in the case of soda lime before the carbon dioxide reaction, but calcium carbonate crystals (Calcite, Aragonite) were grown in the case of soda lime after the carbon dioxide reaction. This means that the weight loss confirmed in the thermogravimetric analysis is due to calcium carbonate. |[0073] FIG. 6 shows thermogravimetric analysis and XRD analysis results for the granular soda-lime-pellet (Example 3) of the present invention. Panel A) shows the results of analyzing the reduction change before and after the carbon dioxide reaction; and Panel B shows the results of the XRD analysis before and after the carbon dioxide reaction. As a result of thermogravimetric analysis of the granular soda-lime-pellet, it was confirmed that a loss of about 20.69 wt. % occurred up to about 600 to 700°C. The above result is believed to be due to the fact that the granular soda-lime-pellet absorbed carbon dioxide and became carbonated. The results are supported by the results of XRD analysis of granular soda-lime-pellets. As a result of XRD analysis of the granular soda lime-pellet, it was confirmed that only lime crystals were found in the case of soda lime before the carbon dioxide reaction, but calcium carbonate crystals (Calcite, Aragonite) were grown in the case of soda lime after the carbon dioxide reaction. This means that the weight loss confirmed in the thermogravimetric analysis is due to calcium carbonate. |[0075] 2) Specific Surface Area, Calcium Carbonate Conversion Rate, and Friability Analysis Results |[0076] Table 4 shows results of analyzing specific surface areas, calcium carbonate conversion rates, and friability of the spherical soda lime-pellet (Example 1), the columnar soda-pellet (Example 2), and the granular soda lime-pellet (Example 3) of the present invention.|[0077] itemExample 1Example 2Example 3manufacturing methoddisk typeextrusion methodmixing methodSpecific surface area (BET, m2/g)9.74604.08087.2005Calcium carbonate Conversion (%)30.7017.4626.33Masondo (Friability, %)1.691.081.23shapespherical shapecolumnar shapegranule shape|[0078] As a result of the analysis, the specific surface area was higher in the order of the spherical soda lime-pellet prepared by the disk method (Example 1), the granular soda lime-pellet prepared by the mixing method (Example 3), and the columnar soda lime-pellet prepared by the extrusion method (Example 2). In addition, it was confirmed that the calcium carbonate conversion rate calculated through the decarboxylation value confirmed through the thermogravimetric analysis was also high in the order of the spherical soda-lime-pellet prepared by the disk method (Example 1), the granular soda-lime-pellet prepared by the mixing method (Example 3), and the columnar soda-lime-pellet prepared by the extrusion method (Example 2) in the same order as the specific surface area. |[0079] The Friability (%) is a method for quantitatively determining a degree to which a product can withstand external impacts generated during transportation and distribution of the product. Soda lime is used to remove carbon dioxide in various fields such as mines, defense industry, medical care, and diving, and in particular, when it is used in a place related to a respiratory system such as medical or diving equipment, there is a concern that an airway disease may occur when dust generated from soda lime is directly inhaled, so it is also important to minimize dust generation in the distribution process by maintaining proper intensity. Thus, in the present invention, the friability was measured using a tablet friability test (see FIG. 7). FIG. 7 shows a Tablet Friability Test method of the present invention. Panel A) shows a schematic diagram of the friability test of the United States Pharmacopeia (UPS); and Panel B) shows the appearance of testing the friability.|[0080] As a result of analyzing the friability, it was confirmed that the spherical soda lime-pellet prepared by the disk method (Example 1), the granular soda lime-pellet prepared by the mixing method (Example 3), and the columnar soda lime-pellet prepared by the extrusion method (Example 2) were high in that order. |[0081] The specific embodiments described herein represent preferred implementations or examples of the present disclosure, and the scope of the present disclosure is not limited thereby. It will be apparent to those skilled in the art that modifications and other uses of the invention do not depart from the scope of the invention set forth in the claims herein. (KR10-2680805)|TECHNICAL FIELD|[0001] The present invention relates to a manufacturing method of soda lime for absorbing carbon dioxide using domestic limestone resources.|BACKGROUND ART|[0003] A technology for capturing carbon dioxide mineralization using soda lime generated from limestone is used in various fields such as medical, leisure, food, environment, military and fisheries industries as well as environmental significance for realizing carbon neutrality. In the medical field, since carbon dioxide is removed from circulating air by being used in a respirator of a patient undergoing anesthesia surgery, the respirator is used to prevent poisoning or oxygen from being deficient, and is also used as an auxiliary tool for preventing hypercarbonemia, hypertension, tachycardia, skin dryness, cardiac arrhythmia, brain blood flow, and increase in brain pressure, which are caused by an excessively high concentration of carbon dioxide. In addition, the leisure industry is used to prevent the concentration of carbon dioxide in the body from increasing in the diving field where divers dive with oxygen bombes. In the food industry, carbon dioxide generated during the decomposition of sugar and protein under oxygen-free conditions by microorganisms is removed in industries such as liquor, kimchi, and fermented soybean, using a fermentation process, and thus the present invention can be used to prevent expansion, explosion, or damage of packaging materials due to carbon dioxide generated during the distribution process.|[0004] Korean Patent Application No. 10-2004-0013047 discloses a size, hardness, drying loss, and carbon dioxide absorption capacity of soda lime particles; Korean Patent Application No. 10-2008-010367 discloses a method for preparing a carbon dioxide adsorbent having a porous channel using X13 zeolite, lithium hydroxide, and soda lime; and Korean Patent Registration No. 10-2438061 discloses a method for using soda lime to react with carbon dioxide in an exhaust gas discharge part such as a boiler, a limestone firing furnace, a drying furnace, and an incinerator exhaust gas of a papermaking process and to separate and recover the same in the form of carbonate. However, the prior art does not specifically disclose a method for preparing a form of soda lime, which is an important factor for determining carbon dioxide absorption performance. In general, soda lime is used by preparing a bulk cured body and then grinding it to a certain size. In particular, when it is manufactured from a fine powder, the specific surface area increases, thereby improving the efficiency of carbon dioxide removal. However, when fine dust generated in the pulverization process and fine dust generated in cracks of particles are present, the fine dust is inhaled into the respiratory tract to cause inflammation or remain in food to deteriorate marketability, and thus it has to be removed through a complicated process. In addition, in order to prevent dust from being generated due to being destroyed during use, the soda lime powder should be manufactured with a certain strength or more, which makes grinding more difficult, thereby causing a problem in that the production yield of soda lime is lowered and production costs are increased. |[0005] The patent documents and references referred to herein are incorporated herein by reference to the same extent that each document is individually and clearly specified by reference. |CITATION LIST|PATENT LITERATURE|[0007] Korean Patent Application No. 10-2004-0013047|Korean Patent Application No. 10-2008-010367|Korean Patent Registration 10-2438061|SUMMARY OF INVENTION|TECH PROBLEM|[0008] To solve the above-described problems, the present invention provides a method for manufacturing soda-lime pellets, wherein the sodalime pellets have a specific surface area which is improved into several ㎜ of a spherical shape, granules, or pillars, by using an additive for improving a specific surface area and an additive for improving strength, without an artificial specific surface area improvement process through a separate grinding process, and can prevent cracks or the like which occur during use.|[0009] Accordingly, it is an object of the present invention to provide a method for producing soda-lime pellets having a spherical shape, a granular shape or a columnar shape with an improved specific surface area using a disk pelletizing apparatus, an extrusion pelletizing apparatus or a mixing pelletizing apparatus.|[0010] Other objects and technical features of the present invention will be more specifically presented by the following detailed description of the present invention, claims, and drawings. |TECH SOLUTION|[0012] The present invention provides a method for preparing a multi-layered carbon dioxide sorbent, the method comprising: a first step of preparing a first alkaline aqueous solution with a pH of 13 or higher, the first alkaline aqueous solution including sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet; a second step of preparing a second alkaline aqueous solution with a pH of 13 or higher, in which any one viscous agent selected from the group consisting of sodium polyacrylate, gelatin, and agar as a viscous agent, or two or more viscous agents are dissolved in the first alkaline aqueous solution; a third step of preparing a slaked lime powder mixture prepared by mixing any one additive or two or more additives selected from the group consisting of active carbon and expanding clay, such as Montmorillonite, Bentonite, vermiculite, and zeolite, as an additive for improving the non-surface; and a fourth step of mixing the first alkaline aqueous solution or the second alkaline aqueous solution with the slaked lime water to prepare a pellet-absorbing mixture for absorbing carbon dioxide gas.|[0013] The soda lime pellets for absorbing carbon dioxide are characterized by including: a 4-1 step of tilting the cylindrical disk of a disk pelletizing apparatus, putting the slaked lime powder mixture in the cylindrical disk, rotating the same, and mixing the same; a 4-2 step of spraying the first alkaline aqueous solution or the second alkaline aqueous solution into the slaked lime powder mixture mixed in the cylindrical disk to grow spherical soda lime pellets; and a 4-3 step of obtaining spherical soda lime pellets having a diameter of 2-4 ㎜.|[0014] The slaked lime powder mixture is characterized in that the cylindrical disk of the disk pelletizing apparatus is rotated under the conditions of a slope of 30 to 50° and a stirring speed of 20 to 30rpm, and the first alkaline aqueous solution or the second alkaline aqueous solution is sprayed at 5 to 9 ㎖/min.|[0015] The method of preparing soda lime-pellets for carbon dioxide absorption may include: step 4-4 of mixing the slaked lime powder mixture with the first alkaline aqueous solution or the second alkaline aqueous solution to prepare slaked lime dough for extrusion; step 4-5 of preparing cylindrical soda-lime-pellets having an average diameter of 4 ㎜ in an extrusion type pelletizing apparatus; and step 4-6 of drying and then cutting the cylindrical soda-lime-pellets to obtain pillar-shaped soda-lime-pellets having an average diameter of 4 ㎜ and an average length of 10 ㎜.|[0016] In addition, the method of preparing soda lime pellets for absorbing carbon dioxide includes: step 4-7 of preparing granular soda lime seeds by adding the first alkaline aqueous solution or the second alkaline aqueous solution while primarily stirring the slaked lime powder mixture in a mixing bowl of a mixing pelletizing apparatus; and step 4-8 of preparing granular soda lime-pellets by secondarily stirring the granular soda lime seeds.|[0017] The primary stirring may be performed at 52 to 72rpm. for 2 to 5 minutes, and the secondary stirring may be performed at 110 to 140rpm. for 1 to 5 minutes.|[0018] The ethyl violet expresses purple when the pH of the soda lime for absorbing carbon dioxide is lowered to 10 or less to indicate that the absorption capacity of the soda lime for absorbing carbon dioxide is lowered, and the soda lime for absorbing carbon dioxide has a specific surface area of 4 to 10 m2/g, a conversion rate of calcium carbonate of 15 to 32%, and friability of 0.9 to 1.8%.|ADVANTAGEOUS EFFECTS|[0020] The present invention uses an additive for improving a specific surface area and an additive for improving strength to not only have an excellent carbon dioxide removal rate without an artificial specific surface area improvement process through a separate crushing process but also prevent cracks or the like which are generated during use. In a manufacturing method, soda lime pellets having a ㎜ level of spherical shape, granular shape or columnar shape with an improved specific surface area are manufactured using a disk pelletizing apparatus, an extrusion pelletizing apparatus or a mixing pelletizing apparatus.|DESCRIPTION OF DRAWINGS|[0022] FIG. 1 shows a disk pelletizing apparatus of the present invention. FIG. 2 shows an extrusion pelletizing apparatus of the present invention. FIG. 3 shows the mixing pelletizing apparatus of the present invention. FIG. 4 shows thermogravimetric analysis and XRD analysis results of spherical soda-lime-pellet of the present invention. FIG. 5 shows thermogravimetric analysis and XRD analysis results for the pillar-shaped soda lime-pellet of the present invention. FIG. 6 shows thermogravimetric analysis and XRD analysis results for the granular soda-lime-pellet of the present invention. FIG. 7 shows a Tablet Friability Test method of the present invention.|DESCRIPTION OF EMBODIMENTS|[0023] The present invention provides a method for preparing a multi-layered carbon dioxide sorbent, the method comprising: a first step of preparing a first alkaline aqueous solution having a pH of 13 or higher, the first alkaline aqueous solution including sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet; a second step of preparing a second alkaline aqueous solution having a pH of 13 or higher, in which any one viscosity agent selected from the group consisting of sodium polyacrylate, gelatin, and agar as a viscosity agent, or two or more viscosity agents are dissolved in the first alkaline aqueous solution; a third step of preparing a slaked lime powder mixture prepared by mixing any one additive or two or more additives selected from the group consisting of montmorillonite, bentonite, vermiculite and active carbon, the additive serving as a non-surface enhancing additive, with the second alkaline aqueous solution; and a fourth step of mixing the slaked lime powder mixture with the second alkaline aqueous solution and pelletizing the mixture to prepare a multi-layered carbon dioxide sorbent pellet.|[0024] The soda lime of the present invention is manufactured by using lime as a main component and adding sodium hydroxide (NaOH), potassium hydroxide (KOH), and the like, and has a property of absorbing carbon dioxide in the atmosphere. A small amount of hydroxides such as sodium (Na), potassium (K), lithium (Li), and the like are added to the soda lime for absorbing carbon dioxide, and this serves as a catalyst for converting calcium hydroxide to calcium carbonate (CaCO3) by absorbing carbon dioxide. Sodalime used for medical purposes is practically unused or used in a very small amount because lithium is expensive compared to sodium and potassium hydroxides. |[0025] The reaction in which the soda lime absorbs carbon dioxide is the same as Chemical Formulas (1) and (2), and sodium hydroxide is repeatedly extinguished and regenerated until calcium hydroxide is all converted to calcium carbonate.|[0026] |[0027] |[0028] The soda lime for absorbing carbon dioxide of the present invention can be prepared in the form of pellets at a ㎜ level without any additional pulverization, and specifically, can be prepared by a disk pelletizing apparatus, an extrusion pelletizing apparatus, or a mixing pelletizing apparatus. |[0029] When a disk pelletizing apparatus is used, the method for manufacturing soda-lime pellets for absorbing carbon dioxide may be a manufacturing method, comprising: a step 4-1 of tilting the cylindrical disk of the disk pelletizing apparatus, and then inserting and rotating and mixing the slaked lime powder mixture; a step 4-2 of spraying the second alkaline aqueous solution to the slaked lime powder mixture mixed in the cylindrical disk so as to grow spherical soda-lime pellets; and a step 4-3 of obtaining spherical soda-lime pellets having a diameter of 2 to 4 ㎜. The slaked lime powder mixture is characterized in that the cylindrical disk of the disk pelletizing apparatus is rotated under the conditions of a slope of 30 to 50° and a stirring speed of 20 to 30rpm, and the second alkaline aqueous solution is sprayed at 5 to 9 ㎖/min. If the conditions are not satisfied, it may be difficult to achieve the desired size of the pellets due to difficulty in agglomeration, which may take more time to reach the desired size of the pellets, or it may be difficult to adjust the size of the pellets due to excessive agglomeration. |[0030] When an extrusion-type pelletizing apparatus is used, the method of manufacturing the soda lime pellets for absorbing carbon dioxide may include: step 4-4 of mixing the slaked lime powder mixture with the first alkaline aqueous solution or the second alkaline aqueous solution to prepare slaked lime dough for extrusion; step 4-5 of drying the slaked lime dough in an extrusion-type pelletizing apparatus to prepare cylindrical soda lime-pellets having an average diameter of 4 ㎜; and step 4-6 of drying and cutting the cylindrical soda lime-pellets to obtain cylindrical soda lime-pellets having an average diameter of 4 ㎜ and an average length of 10 ㎜. |[0031] When the mixing pelletizing apparatus is used, the method of preparing the soda lime pellets for absorbing carbon dioxide may include: step 4-7 of preparing granular soda lime seeds by adding the first alkaline aqueous solution or the second alkaline aqueous solution while primarily stirring the slaked lime powder mixture in the mixing bowl of the mixing pelletizing apparatus; and step 4-8 of preparing granular soda lime-pellets by secondarily stirring the granular soda lime seeds and increasing strength. The primary stirring may be performed at 52 to 72rpm. for 2 to 5 minutes, and the secondary stirring may be performed at 110 to 140rpm. for 1 to 5 minutes. If the above conditions are not satisfied, an appropriate granular soda-lime seed may not be formed, and thus, a pellet may not be prepared. |[0032] In the sodalime of the present invention, a small amount of an ethyl violet may be added so that the carbon dioxide absorption limit may be checked with the naked eye. At this time, the indicator forms carbonic acid along with moisture while the soda lime absorbs carbon dioxide, and accordingly, as the pH falls below 10, the color of the soda lime turns purple, which is an indicator of whether the soda lime loses its ability to absorb carbon dioxide. |[0033] The soda lime for absorbing carbon dioxide of the present invention has a specific surface area of 4 to 10 m2/g, a calcium carbonate conversion rate of 15 to 32%, and friability of 0.9 to 1.8%. |[0034] Hereinafter, the present invention will be described in detail with reference to Examples. |[0036] embodiment |[0038] 1. Methods of experiment; |[0039] 1) Preparation of Alkaline Aqueous Solution |[0040] In the present invention, soda lime was prepared by using an alkaline aqueous solution. The alkaline aqueous solution is mixed with Slaked lime (Ca(OH)2) and serves as a catalyst for reaction with carbon dioxide (CO2) and a limit indicator of the reaction. First, a first alkaline aqueous solution was prepared. A first alkaline aqueous solution was prepared by dissolving sodium hydroxide (NaOH), potassium hydroxide (KOH), and ethyl violet (EV, Ethyl violet) in water at an appropriate ratio and a pH of 13 or higher. |[0041] The ethyl violet is used as a pH indicator of soda lime of the present invention. Soda lime absorbs carbon dioxide to form water and carbonic acid. As a result, the pH decreases to less than 10, which means that the soda lime lost its ability to absorb carbon dioxide. Conventional indicators monitor the pH change in the solution phase. In the present invention, since the soda lime is prepared by adding ethyl violet as an indicator, the soda lime absorbs carbon dioxide sufficiently and becomes purple when the pH is below 10, thereby indicating the loss of carbon dioxide removal ability. Since the ethyl violet does not have good solubility in water, when a solid sample is used, it should be diluted in an organic solvent including an OH group such as ethanol or methanol. Therefore, in the present invention, 0.1% ethyl violet diluted in methanol was used.|[0042] In order to increase the strength of the soda lime, a viscous agent was added to the first alkaline aqueous solution to prepare a second alkaline aqueous solution, and then reacted with lime. |[0043] As the viscosity agent, a material such as Sodium polyacrylate (SPA), gelatin, agar, or the like, which improves viscosity and increases stability of colloidal materials may be used, and preferably, Sodium polyacrylate (SPA) may be used. In the present invention, SPA was added in an amount of 0.1 to 0.3 parts by weight based on 100 parts by weight of the first alkaline aqueous solution and then mixed to prepare a second alkaline aqueous solution. The viscous material has the effect of increasing the strength of soda lime.|[0044] Table 1 below shows the composition of the first alkaline aqueous solution of the present invention, and Table 2 shows the composition of the second alkaline aqueous solution of the present invention.|[0045]  ingredientcomposition ratiofirst alkaline aqueous solutionsodium hydroxide 10 wt.% potassium hydroxide8 wt.% 0.1% ethyl violet solution12 wt.% water70 wt.%|TABLE 2|[0046]  ingredientcomposition ratiosecond alkaline aqueous solutionfirst alkaline aqueous solution100 parts by weight sodium polyacrylate0.1 to 0.3 parts by weight|[0048] 2) Preparation of Slaked Lime Powder Mixture |[0049] The second alkaline aqueous solution prepared above and the slaked lime powder mixture were mixed to prepare soda lime and pelletized in the preparation process. |[0050] In the slaked lime powder mixture of the present invention, a specific surface enhancing additive was used in order to increase the specific surface area of soda lime to improve reactivity with carbon dioxide. As the additive for enhancing non-surface, clay minerals or active carbon may be used. Since the clay mineral expands in volume by meeting moisture and contracts again during drying, the clay mineral has an effect of increasing the specific surface area of soda lime, and montmorillonite, bentonite, or vermiculite may be used. In the present invention, bentonite was used as the additive for enhancing the specific surface, and the additive for enhancing the specific surface may be used in a weight ratio of slaked lime: the additive for enhancing the specific surface=80 to 90: 20 to 10.|[0051] Table 3 below shows the composition of the slaked lime powder mixture of the present invention.|[0052]  ingredientcontentslaked lime powder mixtureslaked lime (Ca(OH)2)87.8 wt % bentonite12.2 wt %|[0053] In the present invention, a method of pelletizing by mixing the above raw materials was developed. The pelletizing method was manufactured in three types, such as a disk type, an extruder type, and a mixing type. Sodalime made in a certain shape was dried at 105°C for about 2 hours to secure strength, and the performance of the product was tested. |[0055] (1) Preparation of Soda Lime Using Disk Method |[0056] Spherical soda lime-pellet (Example 1) was prepared using a disk pelletizing apparatus (see FIG. 1). FIG. 1 shows a disk pelletizing apparatus of the present invention. Panel A) shows a disk pelletizing apparatus; panel B) schematically shows controlling the angle of the cylindrical disks of the disk pelletizing apparatus; panel C) schematically shows controlling the rotational speed of the cylindrical disks of the disk pelletizing apparatus and discharging spherical soda lime-pellets; and panel D) shows spherical soda lime-pellets prepared through the disk pelletizing apparatus. 410g (360g of slaked lime and 50 g of a non-surface enhancing additive) of a slaked lime powder mixture was put in a cylindrical disk (diameter of 400 ㎜) of a disk pelletizing apparatus, and the disk was rotated under conditions of a slope of 40° and a stirring speed of 25rpm. When the disk rotates, the slaked lime powder mixture rises along the surface of the disk and then flows down along the inclined surface by gravity. In this case, the first alkaline aqueous solution or the second alkaline aqueous solution was sprayed at 7 ㎖/min to prepare a soda-lime seed in which a droplet and a raw material were bonded. The soda lime seed is grown in a spherical shape while repeating the up-and-down motion along the rotating disk wall, and when it becomes a certain size and weight, it is discharged without further participating in the up-and-down motion. Among the discharged soda lime, small particles that are not used in the product can be recycled as soda lime seeds in the manufacturing process through sieving. In the present invention, a spherical sodalime-pellet having a diameter of 2 to 4 ㎜ was prepared by using the method.|[0058] (2) Preparation of Soda Lime by Extrusion |[0059] A columnar soda lime-pellet (Example 2) was prepared using an extrusion-type pelletizing apparatus (see FIG. 2). FIG. 2 shows an extrusion pelletizing apparatus of the present invention. Panel A) shows an extrusion pelletizing apparatus; and Panel B) shows columnar soda lime-pellets made using the extrusion pelletizing apparatus. First, the slaked lime powder mixture and the first alkaline aqueous solution or the second alkaline aqueous solution were mixed to prepare a slaked lime dough for extrusion. The first or second alkaline aqueous solution was put into a mixer bowl and stirred at a rotation speed of 62rpm for 5 minutes while adding a slaked lime powder mixture to prepare a slaked lime dough for extrusion. The slaked lime dough for extrusion was put into an extrusion-type pelletizing apparatus, and then, an inner screw feeder was rotated to slowly push it out to an extrusion unit, and a perforated plate having an average diameter of 4 ㎜ was mounted on the extrusion unit to prepare cylindrical soda lime-pellets having a diameter of 4 ㎜ (see FIG. 2). different perforated plates have different diameters to produce column-shaped sodalime-pellets of different diameters. The prepared pillar-shaped soda lime-pellets were dried at 105°C. for 2 hours or more and then cut to prepare pillar-shaped soda lime-pellets having an average diameter of 4㎜ and an average length of 10㎜.|[0061] (3) Preparation of Soda Lime Using Mixer Method |[0062] Granular soda-lime-pellet (Example 3) was prepared using a mixing pelletizing apparatus (see FIG. 3). FIG. 3 shows the mixing pelletizing apparatus of the present invention. Panel A) shows a mixing pelletizing apparatus; Panel B) shows granular soda lime-pellets prepared using the mixing pelletizing apparatus. First, the slaked lime powder mixture was put into a mixing bowl, and then a second alkaline aqueous solution was added while stirring the mixing paddle at a low speed (primary stirring) to prepare a granular soda-lime seed and then stirred at a high speed (secondary stirring) to prepare a granular soda-lime-pellet. |[0063] The mixing paddle performs rotation and revolution motions in the mixing bowl. The slaked lime powder mixture and the second alkaline aqueous solution are agglomerated while colliding with the mixer bowl wall and the mixer paddle to produce a granular soda-lime seed. The size of the granular soda-lime seed is determined according to the interval between the mixer paddle and the mixer bowl, and the cohesive strength of the granular soda-lime seed is determined according to the stirring speed. The granular soda-lime seed was sufficiently stirred to grow to a desired size, and after reaching the desired size, the stirring speed was increased to improve the cohesion of the granular soda-lime. |[0064] In the present invention, the interval between the mixer paddle and the mixer bowl was adjusted to 10 to 15 ㎜, and a slaked lime powder mixture and a second alkaline aqueous solution were added and stirred at low speed (62 rpm) for 2 to 5 minutes to prepare a granular soda-lime seed having a diameter of 10mm or less. Then, the mixture was stirred at high speed for 1 to 5 minutes (125 rpm) to prepare a granular soda lime.|[0066] 2. Results of experiments; |[0067] The spherical soda-lime-pellet (Example 1), the columnar soda-lime-pellet (Example 2), and the granular soda-lime-pellet (Example 3) were sieved to obtain a sample having a particle size of 2 to 4 ㎜. The sample was reacted for 20 minutes at a flow rate of 1L/min with 99% CO2 gas. The samples were subjected to Thermogravimetric Analysis (TGA), X-Ray Diffraction pattern (XRD), Brunauer-Emmett-Teller analysis (BET), and Masson Friability. The physical properties of the sample were measured before the reaction, and the calcium carbonate (CaCO3) conversion rate and strength were evaluated through the analysis after the reaction.|[0069] 1) Results of Thermogravimetric Analysis and X-ray Diffraction Analysis |[0070] As a result of thermogravimetric analysis on the soda lime of the present invention in which carbon dioxide was reacted, it was confirmed that the weight was reduced by the bound water at about 400°C in common. In the case of soda lime before the carbon dioxide reaction, the weight reduction characteristics were shown by the bound water, and in the case of soda lime after the carbon dioxide reaction, the weight reduction curve by the decarboxylation reaction of typical calcium carbonate was shown at about 600°C.|[0071] FIG. 4 shows thermogravimetric analysis and XRD analysis results of spherical soda-lime-pellet of the present invention. Panel A) shows the results of analyzing the reduction change before and after the carbon dioxide reaction; and Panel B shows the results of the XRD analysis before and after the carbon dioxide reaction. As a result of thermogravimetric analysis of spherical soda-lime-pellet, it was confirmed that a loss of about 24.12 wt. % occurred up to about 600 to 700°C. The above result is considered to be due to the fact that spherical soda lime-pellet absorbed carbon dioxide and became carbonated. The results are supported by the results of XRD analysis of spherical soda-lime-pellet. As a result of XRD analysis of spherical soda lime-pellet, it was confirmed that only lime crystals were found in the case of soda lime before the carbon dioxide reaction, but calcium carbonate crystals (Calcite, Aragonite) were grown in the case of soda lime after the carbon dioxide reaction. This means that the weight loss confirmed in the thermogravimetric analysis is due to calcium carbonate.|[0072] FIG. 5 shows thermogravimetric analysis and XRD analysis results for the columnar soda-lime-pellet (Example 2) of the present invention. Panel A) shows the results of analyzing the reduction change before and after the carbon dioxide reaction; and Panel B shows the results of the XRD analysis before and after the carbon dioxide reaction. As a result of thermogravimetric analysis on the columnar soda-lime-pellet, it was confirmed that a loss of about 13.72 wt.% occurred up to about 600 to 700°C. The above result is believed to be due to the fact that the columnar soda-lime-pellet absorbed carbon dioxide and became carbonated. The above result is supported by the XRD analysis result of columnar soda-lime-pellet. As a result of XRD analysis of the columnar soda lime-pellet, it was confirmed that only lime crystals were found in the case of soda lime before the carbon dioxide reaction, but calcium carbonate crystals (Calcite, Aragonite) were grown in the case of soda lime after the carbon dioxide reaction. This means that the weight loss confirmed in the thermogravimetric analysis is due to calcium carbonate. |[0073] FIG. 6 shows thermogravimetric analysis and XRD analysis results for the granular soda-lime-pellet (Example 3) of the present invention. Panel A) shows the results of analyzing the reduction change before and after the carbon dioxide reaction; and Panel B shows the results of the XRD analysis before and after the carbon dioxide reaction. As a result of thermogravimetric analysis of the granular soda-lime-pellet, it was confirmed that a loss of about 20.69 wt. % occurred up to about 600 to 700°C. The above result is believed to be due to the fact that the granular soda-lime-pellet absorbed carbon dioxide and became carbonated. The results are supported by the results of XRD analysis of granular soda-lime-pellets. As a result of XRD analysis of the granular soda lime-pellet, it was confirmed that only lime crystals were found in the case of soda lime before the carbon dioxide reaction, but calcium carbonate crystals (Calcite, Aragonite) were grown in the case of soda lime after the carbon dioxide reaction. This means that the weight loss confirmed in the thermogravimetric analysis is due to calcium carbonate. |[0075] 2) Specific Surface Area, Calcium Carbonate Conversion Rate, and Friability Analysis Results |[0076] Table 4 shows results of analyzing specific surface areas, calcium carbonate conversion rates, and friability of the spherical soda lime-pellet (Example 1), the columnar soda-pellet (Example 2), and the granular soda lime-pellet (Example 3) of the present invention.|[0077] itemExample 1Example 2Example 3manufacturing methoddisk typeextrusion methodmixing methodSpecific surface area (BET, m2/g)9.74604.08087.2005Calcium carbonate Conversion (%)30.7017.4626.33Masondo (Friability, %)1.691.081.23shapespherical shapecolumnar shapegranule shape|[0078] As a result of the analysis, the specific surface area was higher in the order of the spherical soda lime-pellet prepared by the disk method (Example 1), the granular soda lime-pellet prepared by the mixing method (Example 3), and the columnar soda lime-pellet prepared by the extrusion method (Example 2). In addition, it was confirmed that the calcium carbonate conversion rate calculated through the decarboxylation value confirmed through the thermogravimetric analysis was also high in the order of the spherical soda-lime-pellet prepared by the disk method (Example 1), the granular soda-lime-pellet prepared by the mixing method (Example 3), and the columnar soda-lime-pellet prepared by the extrusion method (Example 2) in the same order as the specific surface area. |[0079] The Friability (%) is a method for quantitatively determining a degree to which a product can withstand external impacts generated during transportation and distribution of the product. Soda lime is used to remove carbon dioxide in various fields such as mines, defense industry, medical care, and diving, and in particular, when it is used in a place related to a respiratory system such as medical or diving equipment, there is a concern that an airway disease may occur when dust generated from soda lime is directly inhaled, so it is also important to minimize dust generation in the distribution process by maintaining proper intensity. Thus, in the present invention, the friability was measured using a tablet friability test (see FIG. 7). FIG. 7 shows a Tablet Friability Test method of the present invention. Panel A) shows a schematic diagram of the friability test of the United States Pharmacopeia (UPS); and Panel B) shows the appearance of testing the friability.|[0080] As a result of analyzing the friability, it was confirmed that the spherical soda lime-pellet prepared by the disk method (Example 1), the granular soda lime-pellet prepared by the mixing method (Example 3), and the columnar soda lime-pellet prepared by the extrusion method (Example 2) were high in that order. |[0081] The specific embodiments described herein represent preferred implementations or examples of the present disclosure, and the scope of the present disclosure is not limited thereby. It will be apparent to those skilled in the art that modifications and other uses of the invention do not depart from the scope of the invention set forth in the claims herein. Family Number|(110482428)|110482428|Abstract|(KR102680805 B1)|The present invention relates to a method for manufacturing soda lime for carbon dioxide absorption, having an excellent carbon dioxide removal rate even without an artificial specific surface area enhancement process through a separate crushing process and also preventing cracks or the like occurring during use by using an additive for enhancing specific surface area and an additive for improving strength. Provided is a method for manufacturing soda lime pellets with a spherical, a granular, or a columnar shape with an improved specific surface area of a millimeter level by using a disk pelletizing device, an extrusion pelletizing device, or a mixing pelletizing device. The soda lime pellets manufactured by the method according to the present invention have the advantage of being immediately usable without an additional grinding process.COPYRIGHT KIPO 2025|CPC codes|(KR102680805 B1)|B01D-053/14/75|B01D-2257/504|B01J-020/04/1|B01J-020/28/019|B01J-020/28/03|B01J-020/28/054|IPC codes|(KR102680805 B1)|B01D-053/14|B01J-020/04|B01J-020/28| Chemical engineering|Environmental technology B01D-053/14/75|B01D-2257/504|B01J-020/04/1|B01J-020/28/019|B01J-020/28/03|B01J-020/28/054 B01D-053/14/75|B01D-2257/504|B01J-020/04/1|B01J-020/28/019|B01J-020/28/03|B01J-020/28/054 B01D-053/14|B01J-020/04|B01J-020/28 B01D-053/14|B01J-020/04|B01J-020/28 KR102438061|KR20180029569|KR20110047302|KR20080010367|KR20040013047 KR102438061 101583313 WHO=Applicant SELF=N|KR20180029569 79157069 WHO=Examiner SELF=N|KR20110047302 34234355 WHO=Examiner SELF=N|KR20080010367 35060122 WHO=Applicant SELF=N|KR20040013047 33829091 WHO=Applicant SELF=N 한국출원특허 10-2004-0013047|한국출원특허 10-2008-010367|한국등록특허 10-2438061 KR20180029569; KR20110047302; KR20040013047; KR20080010367; KR102438061 GRANTED (KR10-2680805)|GRANTED ALIVE (KR10-2680805)|ALIVE (KR10-2680805)|LEGAL DETAILS FOR KR10-2680805|Actual or expected expiration date=2043-03-29|Legal state=ALIVE|Status=GRANTED|Event publication date=2023-03-29|Event code=KR/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=KR KR10-2023-0040905|Application date=2023-03-29|Standardized application number=2023KR-0040905|Event publication date=2024-07-03|Event code=KR/B1|Event indicator=Pos|Event group=Event indicating In Force|Patent specification|Publication country=KR|Publication number=KR10-2680805|Publication stage code=B1|Publication date=2024-07-03|Standardized publication number=KR102680805 (KR10-2680805)|KR https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=TF3wXQSsXsPEtndC+6NzoCq6vml3jfM5bZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=KR0000000007396647&ekey=2181&xpn=KR102680805&kind=B1 https://doi.org/10.8080/1020230040905 https://permalink.orbit.com/RenderStaticFirstPage?XPN=tm4lh7oGu3NHFLmrKlb%252Ff5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT KR (KR10-2680805)|KR (KR10-2680805)|NAME=KOREA INSTITUTE OF LIMESTONE AND ADVANCED MATERIALS , COUNTRY=KR (KR10-2680805)|NAME=KIM, JUNG-HYUN (KR10-2680805)|NAME=CHO JIN SANG|NAME=KIM YOUNG JIN|NAME=KWON SEOK JE|NAME=SEO JUN HYUNG|NAME=KIM YANG SOO 0 1 Titre: (KR10-2680805)|Method for manufacturing soda lime for carbon dioxide absorption Résumé: (KR10-2680805)|The present invention relates to a method for manufacturing soda lime for carbon dioxide absorption, having an excellent carbon dioxide removal rate even without an artificial specific surface area enhancement process through a separate crushing process and also preventing cracks or the like occurring during use by using an additive for enhancing specific surface area and an additive for improving strength. Provided is a method for manufacturing soda lime pellets with a spherical, a granular, or a columnar shape with an improved specific surface area of a millimeter level by using a disk pelletizing device, an extrusion pelletizing device, or a mixing pelletizing device. The soda lime pellets manufactured by the method according to the present invention have the advantage of being immediately usable without an additional grinding process.COPYRIGHT KIPO 2025 113 Abstract gpt-4o-mini no The article focuses on manufacturing soda lime for CO₂ absorption, which does not involve accelerated weathering or mineral carbonation processes.
116 CN202411000248 CN202411000248 CN118993582 112299757 CN118993582 A 2024-11-22 [CN118993582] 2024-07-24 2024-07-24 2024-11-22 (CN118993582)|2044-07-24 (CN118993582)|System and method for capturing and mineralizing converter flue gas CO2 through steel slag-wastewater (CN118993582)|The invention discloses a system and a method for capturing and mineralizing CO2 in converter flue gas by steel slag-wastewater. The method comprises the following steps: step (1), crushing steel slag and grinding into steel slag micro powder with the particle size of less than 150 microns; (2) the steel slag micro powder and the steel mill wastewater are simultaneously placed in mixing equipment for a Ca < 2 + > leaching reaction; (3) conveying the mixed steel slag slurry from which Ca < 2 + > is leached to a mineralization reactor, and meanwhile, introducing converter flue gas to carry out gas-liquid-solid three-phase mineralization reaction; and (4) carrying out solid-liquid separation on the mineralized slurry after the reaction is finished to obtain mineralized steel slag. Compared with a two-phase mineralization reaction, the method has the advantages that the carbon sequestration rate of the steel slag is increased, the mineralization rate of the steel slag is increased, green low-carbon cement can be prepared after the prepared steel slag is mixed with cured cement, the performance of the cement is better, the problems of discharge and recycling of wastes such as the steel slag, wastewater and waste gas are solved, waste discharge is reduced, and energy conservation and environmental protection are facilitated. DONGFANG ELECTRIC DONGFANG BOILER (CN118993582)|DONGFANG ELECTRIC GROUP DONGFANG BOILER CO. LTD. ([CN]) WANG BO|HU SHILEI|LI NA|YANG HUAN|LIANG QUANXUN|DENG YI|ZHUANG YUANFA (CN118993582)|WANG BO|HU SHILEI|LI NA|YANG HUAN|LIANG QUANXUN|DENG YI|ZHUANG YUANFA (CN118993582)|LIU SHIQUAN;CHENGDU JIUDING TIANYUAN INTELLECTUAL PROPERTY AGENCY CO. LTD.|Reg. Nb: 51214 (CN118993582)|Numerous specific details are set forth in the following description in order to provide a better understanding of the invention.|Patent 201911352090.X discloses a method for preparing high-purity nano calcium carbonate by utilizing steel slag, converter flue gas and steel mill wastewater, which has the advantages that waste gas, waste liquid and waste slag generated in the steelmaking process are simultaneously used to prepare nano calcium carbonate, but the performance of the leached steel slag by the process is not stable, and the document does not consider the subsequent treatment of the leached steel slag, so that the recycling utilization or the effective treatment cannot be realized.|The application adopts a three-phase mineralization mode, compared with a two-phase mineralization reaction, the three-phase mineralization method has the advantages that the steel slag raw materials directly participate in a reaction system in the three-phase reaction, so that the conversion rate of active calcium oxide and magnesium in steel slag can be increased, meanwhile, the mass transfer rate of steel slag slurry and converter flue gas is increased by mechanical stirring, and the mineralization carbon fixation rate of the steel slag is improved;| (CN118993582)|1. The method for capturing and mineralizing converter flue gas CO 2 by using steel slag-wastewater is characterized by comprising the following steps: Step (1): crushing and grinding the steel slag into steel slag micro powder smaller than 150 mu m to participate in subsequent reactions; Step (2): simultaneously placing the steel slag micro powder prepared in the step (1) and steel mill wastewater into mixing equipment to be stirred for Ca 2+ leaching reaction, wherein the liquid-solid ratio of the steel mill wastewater to the steel slag micro powder is 10-50 mL:1g, reacting for 20-60 min to obtain mixed steel slag slurry leached with Ca 2+ after the reaction is finished; Step (3): conveying the mixed steel slag slurry for leaching Ca 2+ to a mineralization reactor, and simultaneously introducing converter flue gas to perform gas-liquid-solid three-phase mineralization reaction, wherein the mineralization reaction time is 60-120 min; Step (4): and (3) carrying out solid-liquid separation on the mineralized slurry after the reaction is finished to obtain mineralized steel slag and filtrate. |10. A system for capturing mineralized converter flue gas CO 2 by using steel slag-wastewater, which is characterized by comprising a pulverizer (1), a leaching device (2), a mineralization reactor (3) and a filter (4); Conveying the steel slag micro powder crushed by the crusher into a leaching device (2), and simultaneously introducing cold rolling wastewater into the leaching device (2) to enable the cold rolling wastewater and the steel slag micro powder to be mixed and reacted in the leaching device (2) to generate mixed steel slag slurry; The reacted mixed steel slag slurry is fed from the top of a mineralization reactor (3), converter smoke is introduced from the bottom of the mineralization reactor (3), the rotation speed of a stirrer at the mineralization reactor (3) is controlled, and three-phase mineralization reaction of steel slag, cold-rolled wastewater and converter smoke is carried out in the mineralization reactor (3), so that mineralized steel slag is obtained; filtering and separating the three-phase mineralized reaction product in a filter (4) to obtain mineralized steel slag and filtrate, wherein the mineralized steel slag can be used as a raw material product in the downstream, and part of the filtrate is conveyed back to the leaching device (2) for recycling. | (CN118993582)|The application discloses a system and a method for capturing and mineralizing converter flue gas CO _2 by steel slag-wastewater, comprising the following steps: step (1): crushing and grinding the steel slag to form steel slag micro powder smaller than 150 mu m; step (2): simultaneously placing the steel slag micropowder and steel mill wastewater into mixing equipment to perform Ca 2+ leaching reaction; step (3): conveying the mixed steel slag slurry for leaching Ca 2+ to a mineralization reactor, and simultaneously introducing converter flue gas to perform gas-liquid-solid three-phase mineralization reaction; step (4): and (3) carrying out solid-liquid separation on the mineralized slurry after the reaction is finished to obtain mineralized steel slag.|The invention aims at: aiming at the problem that the prior steel slag, cold rolling wastewater and steel mill flue gas CO _2 are difficult to realize the recycling utilization or the effective disposal, the system and the method for capturing and mineralizing the converter flue gas CO _2 by the steel slag-wastewater are provided, the cooperative treatment of the steel slag, the wastewater and the converter flue gas of the steel mill is realized, the carbon emission in the production process of the steel industry and the subsequent treatment cost of the steel mill wastewater are reduced, and meanwhile, the green low-carbon cement building material is prepared.|The invention relates to the technical field of energy conservation and environmental protection, in particular to a system and a method for capturing and mineralizing converter flue gas CO _2 by steel slag-wastewater.| (CN118993582)|FLUE GAS(100,55)|CONVERTER FLUE GAS(100,52)|MINERALIZATION REACTOR(100,16)|SLAG WASTEWATER COLLECTING(100,1)|STEEL SLAG(71,72)|STEEL SLAG MICROPOWDER(58,1)|LEACHED STEEL SLAG(57,2)|STEEL MILL WASTEWATER(51,16)|CONVERTER SMOKE(51,2)|STEEL SLAG SLURRY(50,25)|SLAG SLURRY(49,7)|STEEL SLAG MICRO POWDER(48,22)|SLAG MICRO POWDER(47,22)|RECYCLING UTILIZATION(47,2)|LEACHING CA(46,3)|MIXED STEEL SLAG SLURRY(45,7)|LEACHING(40,15)|LEACHED STEEL SLAG TREATMENT(40,1)|COLD ROLLING WASTEWATER(38,10)|LEACHING REACTION(36,3)|MINERALIZATION REACTION(36,2)|LEACHED STEEL SLAG PERFORMANCE(35,1)|MINERALIZATION CARBON FIXATION(29,1)|STEEL SLAG COOPERATIVE TREATMENT(28,2)|CRUSHING(25,3)|CURED CEMENT(25,1)|FILTRATE(22,20)|WASTEWATER(22,6)|COLD ROLLED WASTEWATER(22,4)|MINERALIZATION REACTOR BOTTOM(22,3)|SLAG RESIDUE(22,2)|CO OPERATIVE TREATMENT(21,2)|SLURRY(20,3)|DISPOSAL(20,1)|WASTE DISCHARGE(19,1)|MINERALIZATION REACTOR TOP(18,4)|PULVERIZER(18,2)|ENVIRONMENTAL PROTECTION(16,2)|WASTE LIQUID(16,1)|COLD ROLLING(15,10)|THREE PHASE MINERALIZATION REACTION(15,4)|CALCIUM CARBONATE(15,3)|ENERGY CONSERVATION(15,2)|RETURN PROPORTION(15,1)|CEMENT CLINKER(14,15)|CRUSHER(13,9)|RECYCLING(13,8)|STEEL SLAG WASTEWATER TANK(12,4)|MIXING EQUIPMENT(12,3)|STEEL MILL FLUE GAS(12,1)|FILTRATE CONVEYING PUMP(11,6)|SLURRY CONVEYING PUMP(11,6)|SOLID LIQUID SEPARATION(11,3)|CARBON FIXATION(10,8)|STEEL MILL(10,6)|REACTION PRODUCT(10,3)|PRIOR STEEL SLAG(10,1)|GREEN LOW CARBON CEMENT(9,3)|WASTE GAS(9,2)|SLAG RAW MATERIAL(9,1)|STEEL SLAG RAW MATERIAL(9,1)|THREE PHASE MINERALIZATION(9,1)|ACTIVE CALCIUM OXIDE(8,4)|ALKALINE STEEL MILL WASTEWATER(8,3)|DOWNSTREAM UTILIZATION(7,4)|CARBON EMISSION(7,3)|PH VALUE(7,2)|THREE PHASE MINERALIZATION MODE(7,1)|LOW CARBON CEMENT(6,5)|MINERALIZE REACTOR BOTTOM(6,4)|MINERALIZE REACTOR TOP(6,4)|REST FILTRATE(6,4)|STEEL INDUSTRY(6,4)|MINERALIZATION REACTION TIME(6,3)|MASS TRANSFER(6,2)|LIQUID SOLID RATIO(5,7)|CALCIUM OXIDE(5,4)|LEACHING SOLUTION(5,3)|NUMEROUS SPECIFIC DETAIL(5,1)|SLAG RECYCLING(5,1)|STEEL MILL WASTEWATER MINERALIZATION(5,1)|STEEL SLAG MINERALIZATION CAPACITY(5,1)|STEEL SLAG STABILIZATION(5,1)|STIRRER ROTATING SPEED(4,4)|TREATMENT COST(4,4)|CONVERSION RATE(4,3)|ROTATION SPEED(4,3)|CIRCULATION PROPORTION(4,1)|CONVERTER FUME(4,1)|DICALCIUM SILICATE(4,1)|MANUFACTURER ATTENTION(4,1)|THREE PHASE REACTION(4,1)|MIXER(3,6)|ALKALINITY(3,2)|BUILDING MATERIAL(3,2)|TWO PHASE MINERALIZATION REACTION(3,2)|COLLABORATIVE TREATMENT(3,1)|CONVERTER STEEL SLAG(3,1)|HOME INDUSTRY(3,1)|HUNDRED MILLION TON(3,1)|NATIONAL STEEL SLAG YIELD(3,1)|RESOURCE TREATMENT(3,1)|STEEL SLAG REACTION(3,1)|WET MINERALIZATION MEDIUM(3,1)| (CN118993582)|1. The method for capturing and mineralizing converter flue gas CO 2 by using steel slag-wastewater is characterized by comprising the following steps:| Step (1): crushing and grinding the steel slag into steel slag micro powder smaller than 150 mu m to participate in subsequent reactions; | Step (2): simultaneously placing the steel slag micro powder prepared in the step (1) and steel mill wastewater into mixing equipment to be stirred for Ca 2+ leaching reaction, wherein the liquid-solid ratio of the steel mill wastewater to the steel slag micro powder is 10-50 mL:1g, reacting for 20-60 min to obtain mixed steel slag slurry leached with Ca 2+ after the reaction is finished; | Step (3): conveying the mixed steel slag slurry for leaching Ca 2+ to a mineralization reactor, and simultaneously introducing converter flue gas to perform gas-liquid-solid three-phase mineralization reaction, wherein the mineralization reaction time is 60-120 min; | Step (4): and (3) carrying out solid-liquid separation on the mineralized slurry after the reaction is finished to obtain mineralized steel slag and filtrate. |2. The method for capturing and mineralizing converter flue gas CO 2 from steel slag-wastewater according to claim 1, wherein the ratio of the volume flow rate of the converter flue gas to the mixed steel slag slurry in step (3) is 1: 30-50.|3. The method for capturing and mineralizing converter flue gas CO 2 from steel slag-wastewater according to claim 2, wherein the ratio of the volume flow rate of the converter flue gas to the mixed steel slag slurry in step (3) is 1: 30-40.|4. The method for capturing and mineralizing converter flue gas CO 2 by using steel slag-wastewater according to claim 1, wherein in the step (2), the liquid-solid ratio of steel mill wastewater to steel slag micropowder is 20-40 mL:1g, and the mixing reaction time is 20-30 min.|5. The method for capturing and mineralizing converter flue gas CO 2 by using steel slag-wastewater according to claim 1, wherein the mineralization reaction time in the step (3) is 60-90 min.|6. The method for capturing and mineralizing converter flue gas CO 2 by using steel slag-wastewater according to claim 1, wherein the filtrate in the step (4) is returned to the step (2) to be recycled as leaching solution, and the return proportion is 30% -50%.|7. The method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater according to claim 1, further comprising step (5): the mineralized steel slag and the cement clinker are mixed and ground to obtain low-carbon green cement, and the mixing proportion is cement clinker: mineralized steel slag = 80-90: 20 to 10.|8. The method for capturing and mineralizing converter flue gas CO 2 from steel slag-wastewater according to claim 1, wherein the steel mill wastewater in step (2) is cold-rolled wastewater, and the components include Ca 2+:200～300mg/L、Mg2+: 40-100 mg/L, and the pH value is 12-14.|9. The method for capturing and mineralizing converter flue gas CO 2 by using steel slag-wastewater according to claim 1, wherein in the step (3), the converter flue gas is CO 2 converter flue gas with the temperature of 50-70 ℃ and the volume percentage of 20% -30%.|10. A system for capturing mineralized converter flue gas CO 2 by using steel slag-wastewater, which is characterized by comprising a pulverizer (1), a leaching device (2), a mineralization reactor (3) and a filter (4);| Conveying the steel slag micro powder crushed by the crusher into a leaching device (2), and simultaneously introducing cold rolling wastewater into the leaching device (2) to enable the cold rolling wastewater and the steel slag micro powder to be mixed and reacted in the leaching device (2) to generate mixed steel slag slurry; | The reacted mixed steel slag slurry is fed from the top of a mineralization reactor (3), converter smoke is introduced from the bottom of the mineralization reactor (3), the rotation speed of a stirrer at the mineralization reactor (3) is controlled, and three-phase mineralization reaction of steel slag, cold-rolled wastewater and converter smoke is carried out in the mineralization reactor (3), so that mineralized steel slag is obtained; | filtering and separating the three-phase mineralized reaction product in a filter (4) to obtain mineralized steel slag and filtrate, wherein the mineralized steel slag can be used as a raw material product in the downstream, and part of the filtrate is conveyed back to the leaching device (2) for recycling. (CN118993582)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of energy conservation and environmental protection, in particular to a system and a method for capturing and mineralizing converter flue gas CO 2 by steel slag-wastewater.|BACKGROUND ART|[0002] The statements in this section merely provide background information related to the present disclosure and may not constitute prior art.|[0003] The steel industry is one of main carbon emission sources of domestic industry, steel slag is main waste slag produced in the steelmaking process, the national steel slag yield in 2020 reaches 1.6 hundred million tons, but the comprehensive utilization rate is only 30%, and the steel slag stabilization and resource treatment technology is urgently needed. The steel park emits a large amount of flue gas CO 2 gas every year, the steel slag contains dicalcium silicate, f-CaO, f-MgO and other substances, the steel slag mineralization technology can convert active calcium oxide and other substances into stable calcium carbonate, and solid waste treatment and carbon emission reduction synergistic treatment can be realized. Meanwhile, the high-calcium-content wastewater (such as cold-rolled wastewater) generated in the steelmaking process is required to be treated by a set of complete pretreatment processes such as calcium and magnesium removal, and in the steel slag mineralization technology, the cold-rolled wastewater is adopted as a wet mineralization medium, so that the water resource requirement can be reduced, the mineralization process can be enhanced by salinity in the steel mill wastewater, and the steel slag mineralization capacity can be improved. Meanwhile, after a certain amount of pollutants such as calcium ions, alkalinity and salt substances are consumed in the wastewater, the subsequent wastewater treatment difficulty and treatment cost are reduced.|[0004] The high-calcium-content wastewater produced by the steelmaking process, such as cold rolling wastewater, slag and steel mill wastewater mineralization capturing converter flue gas, can realize CO 2 capturing, recycling of the slag and collaborative treatment of low-cost green treatment of the steel mill wastewater, and provides technical support for industrial application of the slag mineralization technology. Patent 201911352090.X discloses a method for preparing high-purity nano calcium carbonate by utilizing steel slag, converter flue gas and steel mill wastewater, which has the advantages that waste gas, waste liquid and waste slag generated in the steelmaking process are simultaneously used to prepare nano calcium carbonate, but the performance of the leached steel slag by the process is not stable, and the document does not consider the subsequent treatment of the leached steel slag, so that the recycling utilization or the effective treatment cannot be realized. Therefore, the method for capturing the flue gas CO 2 of the steel plant by mineralizing the wastewater of the steel plant by utilizing the steel slag mixed with the steel plant is explored, so that the economic and effective three-waste cooperative treatment of the steel industry is realized, and the method has great significance to the steel production process.|DISCLOSURE|Disclosure of Invention|[0005] The invention aims at: aiming at the problem that the prior steel slag, cold rolling wastewater and steel mill flue gas CO 2 are difficult to realize the recycling utilization or the effective disposal, the system and the method for capturing and mineralizing the converter flue gas CO 2 by the steel slag-wastewater are provided, the cooperative treatment of the steel slag, the wastewater and the converter flue gas of the steel mill is realized, the carbon emission in the production process of the steel industry and the subsequent treatment cost of the steel mill wastewater are reduced, and meanwhile, the green low-carbon cement building material is prepared.|[0006] The technical scheme of the invention is as follows:|[0007] a method for capturing mineralized converter flue gas CO 2 by steel slag-wastewater comprises the following steps: |[0008] (1) Crushing and grinding the steel slag to prepare steel slag micro powder, wherein the steel slag micro powder with the preferable grain size less than 150 microns participates in the subsequent reaction; |[0009] (2) Simultaneously placing steel slag micro powder and steel mill wastewater in mixing equipment to be stirred for Ca 2+ leaching reaction, wherein the liquid-solid ratio of the steel mill wastewater to the steel slag micro powder is 10-50 mL:1g, reacting for 20-60 min to obtain mixed steel slag slurry leached with Ca 2+ after the reaction is finished; |[0010] the preferable liquid-solid ratio of the steel mill wastewater to the steel slag micro powder is 20-40 mL:1g, and the mixing reaction time is 20-30min. |[0011] (3) The mixed steel slag slurry for leaching Ca 2+ is conveyed to a mineralizing reactor through a pump, and simultaneously converter flue gas at 50-70 ℃ is introduced to carry out gas-liquid-solid three-phase mineralizing reaction, wherein the mineralizing reaction time is 60-120 min.|[0012] Preferably, the mineralization reaction time is 60 to 90 minutes. Preferably, the converter fume in the step (3) is preferably 20-30% of CO 2 converter fume by volume.|[0013] (4) Carrying out solid-liquid separation on the mineralized slurry after the reaction is finished to obtain mineralized steel slag and filtrate, and returning the filtrate to the step (2) to be used as leaching liquid for recycling;|[0014] preferably, the method further comprises the step (5) of mixing and grinding the mineralized steel slag and the cement clinker to obtain the low-carbon green cement, wherein the mixing proportion is that the cement clinker: mineralized steel slag = 80-90: 20-10%, and the strength of the cement is improved by 5-10% after mixing. |[0015] According to a preferred embodiment, the steel slag preferred in step (1) is a converter steel slag, wherein the CaO content is about 30% to 40%, the MgO content is about 5% to 13%, the SiO 2 content is about 20% to 25%, the Al 2O3 content is about 15% to 20%, and the Fe 2O3 content is about 10% to 15%.|[0016] According to a preferred embodiment, the steel mill waste water in step (2) is preferably cold rolling waste water, the composition of which comprises Ca 2+:200～300mg/L、Mg2+: 40-100 mg/L, and the pH value is 12-14.|[0017] According to a preferred embodiment, the mineralization reactor in step (3) is provided with stirring means at a stirring rate of 80-120 rpm, preferably at a rotation speed of 100-120 rpm.|[0018] According to a preferred embodiment, in step (3), the mixed steel slag slurry is pumped from the top of the mineralization reactor, the converter flue gas is added from the bottom of the mineralization reactor, and the volume flow ratio of the mixed steel slag slurry to the converter flue gas is 1: 30-50; preferably 1: 30-40.|[0019] According to a preferred embodiment, in the step (4), mineralized steel slag slurry is filtered and separated to obtain mineralized steel slag and filtrate, the mineralized steel slag is mixed with cement clinker to obtain low-carbon cement, the filtrate can be recycled to the step (2), the recycling proportion is 30% -50%, and the rest filtrate is conveyed to a steel mill wastewater pipe network. The preferred circulation proportion is 40% to 50%.|[0020] In another aspect, the invention provides a system for capturing CO 2 in mineralized converter flue gas by using steel slag-wastewater, which comprises a pulverizer, a leaching device, a mineralization reactor and a filter;|[0021] conveying the steel slag micro powder crushed by the crusher into a leaching device, and simultaneously introducing cold rolling wastewater into the leaching device to enable the cold rolling wastewater and the steel slag micro powder to be mixed and reacted in the leaching device to generate mixed steel slag slurry; |[0022] The reacted mixed steel slag slurry is fed from the top of a mineralization reactor, converter flue gas is introduced from the bottom of the mineralization reactor, the rotation speed of a stirrer in the mineralization reactor is controlled, and three-phase mineralization reaction of steel slag, cold-rolled wastewater and converter flue gas is carried out in the mineralization reactor, so that mineralized steel slag is obtained. |[0023] Filtering and separating the three-phase mineralized reaction product in a filter to obtain mineralized steel slag and filtrate, wherein the mineralized steel slag can be used as a raw material product in the downstream, and part of the filtrate is conveyed back to the leaching device for recycling.|[0024] Preferably, the method also comprises a mixer, and the obtained mineralized steel slag is conveyed into the mixer to be mixed with cement clinker for grinding to prepare low-carbon green cement.|[0025] Preferably, the system further comprises a slurry conveying pump and a filtrate conveying pump, wherein the reacted mixed steel slag slurry is fed from the top of the mineralization reactor by using the slurry conveying pump;|[0026] Filtering and separating the three-phase mineralized reaction product in a filter to obtain mineralized steel slag and filtrate, wherein the mineralized steel slag can be used as a raw material product in the downstream, and part of the filtrate is conveyed back to the leaching device for recycling through a filtrate conveying pump. |[0027] Compared with the prior art, the invention has the beneficial effects that:|[0028] 1. The application adopts a three-phase mineralization mode, compared with a two-phase mineralization reaction, the three-phase mineralization method has the advantages that the steel slag raw materials directly participate in a reaction system in the three-phase reaction, so that the conversion rate of active calcium oxide and magnesium in steel slag can be increased, meanwhile, the mass transfer rate of steel slag slurry and converter flue gas is increased by mechanical stirring, and the mineralization carbon fixation rate of the steel slag is improved; |[0029] 2. The system and the method for capturing and mineralizing CO 2 in the converter flue gas by using the steel slag-wastewater obviously improve the reaction efficiency of the steel slag and carbon dioxide in the converter flue gas by using the technological means such as premix, gas-liquid-solid three-phase mass transfer reaction and the like, wherein the carbon fixation rate of the steel slag can reach 10% under the optimal technological condition, and the mineralization rate of the steel slag can reach 65%; the alkalinity, ca 2+ and other substances in the steel mill wastewater are fully utilized in the collaborative mineralization process, so that the difficulty and the treatment cost of the subsequent wastewater treatment are effectively reduced; |[0030] 3. The invention provides a system and a method for capturing and mineralizing converter flue gas CO 2 by steel slag-wastewater, and provides a system and a method for CO-producing low-carbon cement by mineralizing steel slag in a steel mill, wastewater and carbon dioxide captured in converter flue gas. The implementation of the invention realizes the cooperative treatment of the steel slag, the wastewater and the converter flue gas of the steel mill, reduces the carbon emission and the subsequent treatment cost of the wastewater of the steel mill in the production process of the steel industry, and simultaneously prepares the green low-carbon cement building material. |DRAWINGS DESCRIPTION|[0031] FIG. 1 is a schematic diagram of a system flow for capturing mineralized converter flue gas CO 2 from steel slag-wastewater.|[0032] Reference numerals: 1-pulverizer, 2-leaching device, 3-mineralization reactor, 4-filter, 5-blendor, 6-slurry delivery pump, 7-filtrate delivery pump.|INVENTION MODE|Detailed Description|[0033] The specific embodiments of the present invention are listed only as examples of the present invention, and the present invention is not limited to the specific embodiments described below. Any equivalent modifications and substitutions of the embodiments described below will be apparent to those skilled in the art, and are intended to be within the scope of the present invention. Accordingly, equivalent changes and modifications are intended to be included within the scope of the present invention without departing from the spirit and scope thereof. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. All reagents or equipment were commercially available as conventional products without the manufacturer's attention. Numerous specific details are set forth in the following description in order to provide a better understanding of the invention. It will be understood by those skilled in the art that the present invention may be practiced without some of these specific details. In other embodiments, methods, means, apparatus and steps well known to those skilled in the art have not been described in detail in order to not obscure the present invention.|[0034] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. Unless otherwise indicated, all units used in this specification are units of international standard, and the numerical values and numerical ranges appearing in the present invention are understood to include systematic errors unavoidable in industrial production.|[0035] The features and capabilities of the present invention are described in further detail below in connection with examples.|[0036] The steel slag adopted in the embodiment of the invention comprises, by mass, 35% of CaO, 6% of MgO and 224%、Al2O317%、Fe2O3% of SiO.|[0037] The concentration of each ion of the cold rolling wastewater adopted in the embodiment of the invention is as follows: ca 2+:260mg/L、Mg2+: 50mg/L, pH 12.|[0038] The converter flue gas adopted in the embodiment of the invention contains 28% CO 2 by volume percent.|[0039] Example 1|[0040] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0041] (1) Crushing the steel slag to obtain steel slag micro powder smaller than 150 microns by using a crusher 1, and participating in subsequent reactions;|[0042] (2) Conveying the steel slag micro powder obtained by crushing in the step (1) and cold rolling wastewater into a leaching device 2 for mixing, wherein the proportion of the cold rolling wastewater to the steel slag micro powder is controlled to be 20mL:1g, mixing reaction time was 20min. |[0043] (3) After the step (1), the steel slag slurry is fed from the top of the mineralizing reactor 3 by using a slurry conveying pump 6, converter flue gas is introduced from the bottom of the mineralizing reactor 3, and the volume flow ratio of the steel slag slurry to the converter flue gas is controlled to be about 1:30, controlling the rotating speed of the stirrer to be 80rpm and controlling the reaction time of the steel slag slurry to be 60min.|[0044] (4) After the step (2), mineralized steel slag slurry is separated by a filter 4 to obtain mineralized steel slag and filtrate, the mineralized steel slag is used as a raw material product for downstream utilization, 30% of the filtrate is returned to the step (1) by a filtrate conveying pump 7 for recycling, and the rest of the filtrate is discharged into a steel slag wastewater tank.|[0045] (5) The mineralized steel slag is obtained through filtration, and can be mixed with cement clinker to prepare low-carbon green cement through grinding by a mixer 5, wherein the mixing mass ratio of the mineralized steel slag to the cement clinker is 20:80, and the strength of the cement after mixing is improved by 5.4%.|[0046] The carbon fixation rate of the steel slag reaches: 5, the mineralization rate of the steel slag, namely the conversion rate of active calcium oxide and magnesium in the steel slag, reaches the following steps: 42%.|[0047] Example 2|[0048] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0049] (1) Crushing the steel slag to obtain steel slag micro powder smaller than 150 microns by using a crusher 1, and participating in subsequent reactions;|[0050] (2) The steel slag micro powder with the particle size less than 150 microns obtained by crushing by the crusher 1 and the waste water of the alkaline steel mill are conveyed into the leaching device 2 to be mixed, and the liquid-solid ratio is controlled to be 30mL:1g, mixing reaction time was 30min. |[0051] (3) After the step (1), the steel slag slurry is fed from the top of the mineralizing reactor 3 by using a slurry conveying pump 6, converter flue gas is introduced from the bottom of the mineralizing reactor 3, and the volume flow ratio of the steel slag slurry to the converter flue gas is controlled to be about 1:30, controlling the rotating speed of the stirrer to be 90rpm and controlling the reaction time of the steel slag slurry to be 75min.|[0052] (4) After the step (2), mineralized steel slag slurry is separated by a filter 4 to obtain mineralized steel slag and filtrate, the mineralized steel slag is used as a raw material product for downstream utilization, and 50% of the filtrate is returned to the step (1) by a filtrate conveying pump 7 for recycling. And discharging the rest filtrate into a steel slag waste water tank.|[0053] (5) The mineralized steel slag is obtained through filtration, and can be mixed with cement clinker to prepare low-carbon green cement through grinding by a mixer 5, wherein the mixing mass ratio of the mineralized steel slag to the cement clinker is 20:80, and the strength of the cement after mixing is improved by 6.2%.|[0054] The carbon fixation rate of the steel slag reaches: 6, the mineralization rate of the steel slag reaches: 47%.|[0055] Example 3|[0056] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0057] (1) Crushing the steel slag to obtain steel slag micro powder smaller than 150 microns by using a crusher 1, and participating in subsequent reactions;|[0058] (2) The steel slag micro powder with the particle size less than 150 microns obtained by crushing by the crusher 1 and the waste water of the alkaline steel mill are conveyed into the leaching device 2 to be mixed, and the liquid-solid ratio is controlled to be 40mL:1g, mixing reaction time 40min. |[0059] (3) After the step (1), the steel slag slurry is fed from the top of the mineralizing reactor 3 by using a slurry conveying pump 6, converter flue gas is introduced from the bottom of the mineralizing reactor 3, and the volume flow ratio of the steel slag slurry to the converter flue gas is controlled to be about 1:40, controlling the rotating speed of the stirrer to be 100rpm and controlling the reaction time of the steel slag slurry to be 90min.|[0060] (4) After the step (2), mineralized steel slag slurry is separated by a filter 4 to obtain mineralized steel slag and filtrate, the mineralized steel slag is used as a raw material product for downstream utilization, and 40% of the filtrate is returned to the step (1) by a filtrate conveying pump 7 for recycling. And discharging the rest filtrate into a steel slag waste water tank.|[0061] (5) The mineralized steel slag is obtained through filtration, and can be mixed with cement clinker to prepare low-carbon green cement through grinding by a mixer 5, wherein the mixing mass ratio of the mineralized steel slag to the cement clinker is 15:85, and the strength of the cement after mixing is improved by 7.8%.|[0062] The carbon fixation rate of the steel slag reaches: 8, the mineralization rate of the steel slag reaches: 55%.|[0063] Example 4|[0064] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0065] (1) Crushing the steel slag to obtain steel slag micro powder smaller than 150 microns by using a crusher 1, and participating in subsequent reactions;|[0066] (2) The steel slag micro powder with the particle size less than 150 microns obtained by crushing by the crusher 1 and the waste water of the alkaline steel mill are conveyed into the leaching device 2 to be mixed, and the liquid-solid ratio is controlled to be 50mL:1g, mixing reaction time was 60min. |[0067] (3) After the step (1), the steel slag slurry is fed from the top of the mineralizing reactor 3 by using a slurry conveying pump 6, converter flue gas is introduced from the bottom of the mineralizing reactor 3, and the volume flow ratio of the steel slag slurry to the converter flue gas is controlled to be about 1:50, controlling the rotating speed of the stirrer to be 120rpm and controlling the reaction time of the steel slag slurry to be 120min.|[0068] (4) After the step (2), mineralized steel slag slurry is separated by a filter 4 to obtain mineralized steel slag and filtrate, the mineralized steel slag is used as a raw material product for downstream utilization, and 50% of the filtrate is returned to the step (1) by a filtrate conveying pump 7 for recycling. And discharging the rest filtrate into a steel slag waste water tank.|[0069] (5) The mineralized steel slag is obtained through filtration, and can be mixed with cement clinker to prepare low-carbon green cement through grinding by a mixer 5, wherein the mixing mass ratio of the mineralized steel slag to the cement clinker is 10:90, and the strength of the cement after mixing is improved by 9.8%.|[0070] The carbon fixation rate of the steel slag reaches: 10%, the mineralization rate of the steel slag reaches: 65%.|[0071] Comparative example 1|[0072] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0073] According to the test parameters of the embodiment 4 of the application, after the leaching solution is separated from slag in the step (3), the leaching solution is sent into a mineralizing reactor 3, and the leaching solution and converter flue gas are used for mineralizing, so that the conversion rate of active calcium oxide and magnesium in steel slag and the carbon fixation rate of the steel slag are 5%, and the mineralization rate of the steel slag is 40%; the separated steel slag has unstable performance and can not be mixed with cement clinker to prepare low-carbon cement.|[0074] The above examples merely illustrate specific embodiments of the application, which are described in more detail and are not to be construed as limiting the scope of the application. It should be noted that it is possible for a person skilled in the art to make several variants and modifications without departing from the technical idea of the application, which fall within the scope of protection of the application. (CN118993582)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of energy conservation and environmental protection, in particular to a system and a method for capturing and mineralizing converter flue gas CO 2 by steel slag-wastewater.|BACKGROUND ART|[0002] The statements in this section merely provide background information related to the present disclosure and may not constitute prior art.|[0003] The steel industry is one of main carbon emission sources of domestic industry, steel slag is main waste slag produced in the steelmaking process, the national steel slag yield in 2020 reaches 1.6 hundred million tons, but the comprehensive utilization rate is only 30%, and the steel slag stabilization and resource treatment technology is urgently needed. The steel park emits a large amount of flue gas CO 2 gas every year, the steel slag contains dicalcium silicate, f-CaO, f-MgO and other substances, the steel slag mineralization technology can convert active calcium oxide and other substances into stable calcium carbonate, and solid waste treatment and carbon emission reduction synergistic treatment can be realized. Meanwhile, the high-calcium-content wastewater (such as cold-rolled wastewater) generated in the steelmaking process is required to be treated by a set of complete pretreatment processes such as calcium and magnesium removal, and in the steel slag mineralization technology, the cold-rolled wastewater is adopted as a wet mineralization medium, so that the water resource requirement can be reduced, the mineralization process can be enhanced by salinity in the steel mill wastewater, and the steel slag mineralization capacity can be improved. Meanwhile, after a certain amount of pollutants such as calcium ions, alkalinity and salt substances are consumed in the wastewater, the subsequent wastewater treatment difficulty and treatment cost are reduced.|[0004] The high-calcium-content wastewater produced by the steelmaking process, such as cold rolling wastewater, slag and steel mill wastewater mineralization capturing converter flue gas, can realize CO 2 capturing, recycling of the slag and collaborative treatment of low-cost green treatment of the steel mill wastewater, and provides technical support for industrial application of the slag mineralization technology. Patent 201911352090.X discloses a method for preparing high-purity nano calcium carbonate by utilizing steel slag, converter flue gas and steel mill wastewater, which has the advantages that waste gas, waste liquid and waste slag generated in the steelmaking process are simultaneously used to prepare nano calcium carbonate, but the performance of the leached steel slag by the process is not stable, and the document does not consider the subsequent treatment of the leached steel slag, so that the recycling utilization or the effective treatment cannot be realized. Therefore, the method for capturing the flue gas CO 2 of the steel plant by mineralizing the wastewater of the steel plant by utilizing the steel slag mixed with the steel plant is explored, so that the economic and effective three-waste cooperative treatment of the steel industry is realized, and the method has great significance to the steel production process.|DISCLOSURE|Disclosure of Invention|[0005] The invention aims at: aiming at the problem that the prior steel slag, cold rolling wastewater and steel mill flue gas CO 2 are difficult to realize the recycling utilization or the effective disposal, the system and the method for capturing and mineralizing the converter flue gas CO 2 by the steel slag-wastewater are provided, the cooperative treatment of the steel slag, the wastewater and the converter flue gas of the steel mill is realized, the carbon emission in the production process of the steel industry and the subsequent treatment cost of the steel mill wastewater are reduced, and meanwhile, the green low-carbon cement building material is prepared.|[0006] The technical scheme of the invention is as follows:|[0007] a method for capturing mineralized converter flue gas CO 2 by steel slag-wastewater comprises the following steps: |[0008] (1) Crushing and grinding the steel slag to prepare steel slag micro powder, wherein the steel slag micro powder with the preferable grain size less than 150 microns participates in the subsequent reaction; |[0009] (2) Simultaneously placing steel slag micro powder and steel mill wastewater in mixing equipment to be stirred for Ca 2+ leaching reaction, wherein the liquid-solid ratio of the steel mill wastewater to the steel slag micro powder is 10-50 mL:1g, reacting for 20-60 min to obtain mixed steel slag slurry leached with Ca 2+ after the reaction is finished; |[0010] the preferable liquid-solid ratio of the steel mill wastewater to the steel slag micro powder is 20-40 mL:1g, and the mixing reaction time is 20-30min. |[0011] (3) The mixed steel slag slurry for leaching Ca 2+ is conveyed to a mineralizing reactor through a pump, and simultaneously converter flue gas at 50-70 ℃ is introduced to carry out gas-liquid-solid three-phase mineralizing reaction, wherein the mineralizing reaction time is 60-120 min.|[0012] Preferably, the mineralization reaction time is 60 to 90 minutes. Preferably, the converter fume in the step (3) is preferably 20-30% of CO 2 converter fume by volume.|[0013] (4) Carrying out solid-liquid separation on the mineralized slurry after the reaction is finished to obtain mineralized steel slag and filtrate, and returning the filtrate to the step (2) to be used as leaching liquid for recycling;|[0014] preferably, the method further comprises the step (5) of mixing and grinding the mineralized steel slag and the cement clinker to obtain the low-carbon green cement, wherein the mixing proportion is that the cement clinker: mineralized steel slag = 80-90: 20-10%, and the strength of the cement is improved by 5-10% after mixing. |[0015] According to a preferred embodiment, the steel slag preferred in step (1) is a converter steel slag, wherein the CaO content is about 30% to 40%, the MgO content is about 5% to 13%, the SiO 2 content is about 20% to 25%, the Al 2O3 content is about 15% to 20%, and the Fe 2O3 content is about 10% to 15%.|[0016] According to a preferred embodiment, the steel mill waste water in step (2) is preferably cold rolling waste water, the composition of which comprises Ca 2+:200～300mg/L、Mg2+: 40-100 mg/L, and the pH value is 12-14.|[0017] According to a preferred embodiment, the mineralization reactor in step (3) is provided with stirring means at a stirring rate of 80-120 rpm, preferably at a rotation speed of 100-120 rpm.|[0018] According to a preferred embodiment, in step (3), the mixed steel slag slurry is pumped from the top of the mineralization reactor, the converter flue gas is added from the bottom of the mineralization reactor, and the volume flow ratio of the mixed steel slag slurry to the converter flue gas is 1: 30-50; preferably 1: 30-40.|[0019] According to a preferred embodiment, in the step (4), mineralized steel slag slurry is filtered and separated to obtain mineralized steel slag and filtrate, the mineralized steel slag is mixed with cement clinker to obtain low-carbon cement, the filtrate can be recycled to the step (2), the recycling proportion is 30% -50%, and the rest filtrate is conveyed to a steel mill wastewater pipe network. The preferred circulation proportion is 40% to 50%.|[0020] In another aspect, the invention provides a system for capturing CO 2 in mineralized converter flue gas by using steel slag-wastewater, which comprises a pulverizer, a leaching device, a mineralization reactor and a filter;|[0021] conveying the steel slag micro powder crushed by the crusher into a leaching device, and simultaneously introducing cold rolling wastewater into the leaching device to enable the cold rolling wastewater and the steel slag micro powder to be mixed and reacted in the leaching device to generate mixed steel slag slurry; |[0022] The reacted mixed steel slag slurry is fed from the top of a mineralization reactor, converter flue gas is introduced from the bottom of the mineralization reactor, the rotation speed of a stirrer in the mineralization reactor is controlled, and three-phase mineralization reaction of steel slag, cold-rolled wastewater and converter flue gas is carried out in the mineralization reactor, so that mineralized steel slag is obtained. |[0023] Filtering and separating the three-phase mineralized reaction product in a filter to obtain mineralized steel slag and filtrate, wherein the mineralized steel slag can be used as a raw material product in the downstream, and part of the filtrate is conveyed back to the leaching device for recycling.|[0024] Preferably, the method also comprises a mixer, and the obtained mineralized steel slag is conveyed into the mixer to be mixed with cement clinker for grinding to prepare low-carbon green cement.|[0025] Preferably, the system further comprises a slurry conveying pump and a filtrate conveying pump, wherein the reacted mixed steel slag slurry is fed from the top of the mineralization reactor by using the slurry conveying pump;|[0026] Filtering and separating the three-phase mineralized reaction product in a filter to obtain mineralized steel slag and filtrate, wherein the mineralized steel slag can be used as a raw material product in the downstream, and part of the filtrate is conveyed back to the leaching device for recycling through a filtrate conveying pump. |[0027] Compared with the prior art, the invention has the beneficial effects that:|[0028] 1. The application adopts a three-phase mineralization mode, compared with a two-phase mineralization reaction, the three-phase mineralization method has the advantages that the steel slag raw materials directly participate in a reaction system in the three-phase reaction, so that the conversion rate of active calcium oxide and magnesium in steel slag can be increased, meanwhile, the mass transfer rate of steel slag slurry and converter flue gas is increased by mechanical stirring, and the mineralization carbon fixation rate of the steel slag is improved; |[0029] 2. The system and the method for capturing and mineralizing CO 2 in the converter flue gas by using the steel slag-wastewater obviously improve the reaction efficiency of the steel slag and carbon dioxide in the converter flue gas by using the technological means such as premix, gas-liquid-solid three-phase mass transfer reaction and the like, wherein the carbon fixation rate of the steel slag can reach 10% under the optimal technological condition, and the mineralization rate of the steel slag can reach 65%; the alkalinity, ca 2+ and other substances in the steel mill wastewater are fully utilized in the collaborative mineralization process, so that the difficulty and the treatment cost of the subsequent wastewater treatment are effectively reduced; |[0030] 3. The invention provides a system and a method for capturing and mineralizing converter flue gas CO 2 by steel slag-wastewater, and provides a system and a method for CO-producing low-carbon cement by mineralizing steel slag in a steel mill, wastewater and carbon dioxide captured in converter flue gas. The implementation of the invention realizes the cooperative treatment of the steel slag, the wastewater and the converter flue gas of the steel mill, reduces the carbon emission and the subsequent treatment cost of the wastewater of the steel mill in the production process of the steel industry, and simultaneously prepares the green low-carbon cement building material. |DRAWINGS DESCRIPTION|[0031] FIG. 1 is a schematic diagram of a system flow for capturing mineralized converter flue gas CO 2 from steel slag-wastewater.|[0032] Reference numerals: 1-pulverizer, 2-leaching device, 3-mineralization reactor, 4-filter, 5-blendor, 6-slurry delivery pump, 7-filtrate delivery pump.|INVENTION MODE|Detailed Description|[0033] The specific embodiments of the present invention are listed only as examples of the present invention, and the present invention is not limited to the specific embodiments described below. Any equivalent modifications and substitutions of the embodiments described below will be apparent to those skilled in the art, and are intended to be within the scope of the present invention. Accordingly, equivalent changes and modifications are intended to be included within the scope of the present invention without departing from the spirit and scope thereof. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. All reagents or equipment were commercially available as conventional products without the manufacturer's attention. Numerous specific details are set forth in the following description in order to provide a better understanding of the invention. It will be understood by those skilled in the art that the present invention may be practiced without some of these specific details. In other embodiments, methods, means, apparatus and steps well known to those skilled in the art have not been described in detail in order to not obscure the present invention.|[0034] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. Unless otherwise indicated, all units used in this specification are units of international standard, and the numerical values and numerical ranges appearing in the present invention are understood to include systematic errors unavoidable in industrial production.|[0035] The features and capabilities of the present invention are described in further detail below in connection with examples.|[0036] The steel slag adopted in the embodiment of the invention comprises, by mass, 35% of CaO, 6% of MgO and 224%、Al2O317%、Fe2O3% of SiO.|[0037] The concentration of each ion of the cold rolling wastewater adopted in the embodiment of the invention is as follows: ca 2+:260mg/L、Mg2+: 50mg/L, pH 12.|[0038] The converter flue gas adopted in the embodiment of the invention contains 28% CO 2 by volume percent.|[0039] Example 1|[0040] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0041] (1) Crushing the steel slag to obtain steel slag micro powder smaller than 150 microns by using a crusher 1, and participating in subsequent reactions;|[0042] (2) Conveying the steel slag micro powder obtained by crushing in the step (1) and cold rolling wastewater into a leaching device 2 for mixing, wherein the proportion of the cold rolling wastewater to the steel slag micro powder is controlled to be 20mL:1g, mixing reaction time was 20min. |[0043] (3) After the step (1), the steel slag slurry is fed from the top of the mineralizing reactor 3 by using a slurry conveying pump 6, converter flue gas is introduced from the bottom of the mineralizing reactor 3, and the volume flow ratio of the steel slag slurry to the converter flue gas is controlled to be about 1:30, controlling the rotating speed of the stirrer to be 80rpm and controlling the reaction time of the steel slag slurry to be 60min.|[0044] (4) After the step (2), mineralized steel slag slurry is separated by a filter 4 to obtain mineralized steel slag and filtrate, the mineralized steel slag is used as a raw material product for downstream utilization, 30% of the filtrate is returned to the step (1) by a filtrate conveying pump 7 for recycling, and the rest of the filtrate is discharged into a steel slag wastewater tank.|[0045] (5) The mineralized steel slag is obtained through filtration, and can be mixed with cement clinker to prepare low-carbon green cement through grinding by a mixer 5, wherein the mixing mass ratio of the mineralized steel slag to the cement clinker is 20:80, and the strength of the cement after mixing is improved by 5.4%.|[0046] The carbon fixation rate of the steel slag reaches: 5, the mineralization rate of the steel slag, namely the conversion rate of active calcium oxide and magnesium in the steel slag, reaches the following steps: 42%.|[0047] Example 2|[0048] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0049] (1) Crushing the steel slag to obtain steel slag micro powder smaller than 150 microns by using a crusher 1, and participating in subsequent reactions;|[0050] (2) The steel slag micro powder with the particle size less than 150 microns obtained by crushing by the crusher 1 and the waste water of the alkaline steel mill are conveyed into the leaching device 2 to be mixed, and the liquid-solid ratio is controlled to be 30mL:1g, mixing reaction time was 30min. |[0051] (3) After the step (1), the steel slag slurry is fed from the top of the mineralizing reactor 3 by using a slurry conveying pump 6, converter flue gas is introduced from the bottom of the mineralizing reactor 3, and the volume flow ratio of the steel slag slurry to the converter flue gas is controlled to be about 1:30, controlling the rotating speed of the stirrer to be 90rpm and controlling the reaction time of the steel slag slurry to be 75min.|[0052] (4) After the step (2), mineralized steel slag slurry is separated by a filter 4 to obtain mineralized steel slag and filtrate, the mineralized steel slag is used as a raw material product for downstream utilization, and 50% of the filtrate is returned to the step (1) by a filtrate conveying pump 7 for recycling. And discharging the rest filtrate into a steel slag waste water tank.|[0053] (5) The mineralized steel slag is obtained through filtration, and can be mixed with cement clinker to prepare low-carbon green cement through grinding by a mixer 5, wherein the mixing mass ratio of the mineralized steel slag to the cement clinker is 20:80, and the strength of the cement after mixing is improved by 6.2%.|[0054] The carbon fixation rate of the steel slag reaches: 6, the mineralization rate of the steel slag reaches: 47%.|[0055] Example 3|[0056] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0057] (1) Crushing the steel slag to obtain steel slag micro powder smaller than 150 microns by using a crusher 1, and participating in subsequent reactions;|[0058] (2) The steel slag micro powder with the particle size less than 150 microns obtained by crushing by the crusher 1 and the waste water of the alkaline steel mill are conveyed into the leaching device 2 to be mixed, and the liquid-solid ratio is controlled to be 40mL:1g, mixing reaction time 40min. |[0059] (3) After the step (1), the steel slag slurry is fed from the top of the mineralizing reactor 3 by using a slurry conveying pump 6, converter flue gas is introduced from the bottom of the mineralizing reactor 3, and the volume flow ratio of the steel slag slurry to the converter flue gas is controlled to be about 1:40, controlling the rotating speed of the stirrer to be 100rpm and controlling the reaction time of the steel slag slurry to be 90min.|[0060] (4) After the step (2), mineralized steel slag slurry is separated by a filter 4 to obtain mineralized steel slag and filtrate, the mineralized steel slag is used as a raw material product for downstream utilization, and 40% of the filtrate is returned to the step (1) by a filtrate conveying pump 7 for recycling. And discharging the rest filtrate into a steel slag waste water tank.|[0061] (5) The mineralized steel slag is obtained through filtration, and can be mixed with cement clinker to prepare low-carbon green cement through grinding by a mixer 5, wherein the mixing mass ratio of the mineralized steel slag to the cement clinker is 15:85, and the strength of the cement after mixing is improved by 7.8%.|[0062] The carbon fixation rate of the steel slag reaches: 8, the mineralization rate of the steel slag reaches: 55%.|[0063] Example 4|[0064] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0065] (1) Crushing the steel slag to obtain steel slag micro powder smaller than 150 microns by using a crusher 1, and participating in subsequent reactions;|[0066] (2) The steel slag micro powder with the particle size less than 150 microns obtained by crushing by the crusher 1 and the waste water of the alkaline steel mill are conveyed into the leaching device 2 to be mixed, and the liquid-solid ratio is controlled to be 50mL:1g, mixing reaction time was 60min. |[0067] (3) After the step (1), the steel slag slurry is fed from the top of the mineralizing reactor 3 by using a slurry conveying pump 6, converter flue gas is introduced from the bottom of the mineralizing reactor 3, and the volume flow ratio of the steel slag slurry to the converter flue gas is controlled to be about 1:50, controlling the rotating speed of the stirrer to be 120rpm and controlling the reaction time of the steel slag slurry to be 120min.|[0068] (4) After the step (2), mineralized steel slag slurry is separated by a filter 4 to obtain mineralized steel slag and filtrate, the mineralized steel slag is used as a raw material product for downstream utilization, and 50% of the filtrate is returned to the step (1) by a filtrate conveying pump 7 for recycling. And discharging the rest filtrate into a steel slag waste water tank.|[0069] (5) The mineralized steel slag is obtained through filtration, and can be mixed with cement clinker to prepare low-carbon green cement through grinding by a mixer 5, wherein the mixing mass ratio of the mineralized steel slag to the cement clinker is 10:90, and the strength of the cement after mixing is improved by 9.8%.|[0070] The carbon fixation rate of the steel slag reaches: 10%, the mineralization rate of the steel slag reaches: 65%.|[0071] Comparative example 1|[0072] Referring to fig. 1, a system and method for capturing mineralized converter flue gas CO 2 from steel slag-wastewater,|[0073] According to the test parameters of the embodiment 4 of the application, after the leaching solution is separated from slag in the step (3), the leaching solution is sent into a mineralizing reactor 3, and the leaching solution and converter flue gas are used for mineralizing, so that the conversion rate of active calcium oxide and magnesium in steel slag and the carbon fixation rate of the steel slag are 5%, and the mineralization rate of the steel slag is 40%; the separated steel slag has unstable performance and can not be mixed with cement clinker to prepare low-carbon cement.|[0074] The above examples merely illustrate specific embodiments of the application, which are described in more detail and are not to be construed as limiting the scope of the application. It should be noted that it is possible for a person skilled in the art to make several variants and modifications without departing from the technical idea of the application, which fall within the scope of protection of the application. Family Number|(112299757)|112299757|Abstract|(CN118993582 A)|The invention discloses a system and a method for capturing and mineralizing CO2 in converter flue gas by steel slag - wastewater . The method comprises the following steps : step ( 1 ) , crushing steel slag and grinding into steel slag micro powder with the particle size of less than 150 microns ; ( 2 ) the steel slag micro powder and the steel mill wastewater are simultaneously placed in mixing equipment for a Ca < 2 + > leaching reaction ; ( 3 ) conveying the mixed steel slag slurry from which Ca < 2 + > is leached to a mineralization reactor , and meanwhile , introducing converter flue gas to carry out gas - liquid - solid three - phase mineralization reaction ; and ( 4 ) carrying out solid - liquid separation on the mineralized slurry after the reaction is finished to obtain mineralized steel slag . Compared with a two - phase mineralization reaction , the method has the advantages that the carbon sequestration rate of the steel slag is increased , the mineralization rate of the steel slag is increased , green low - carbon cement can be prepared after the prepared steel slag is mixed with cured cement , the performance of the cement is better , the problems of discharge and recycling of wastes such as the steel slag , wastewater and waste gas are solved , waste discharge is reduced , and energy conservation and environmental protection are facilitated . |CPC codes|(CN118993582 A)|B01D - 053/62 |B01D - 053/80 |B01D - 2257/504 |B01D - 2258/0283 |IPC codes|(CN118993582 A)|B01D - 053/62 |B01D - 053/80 | Environmental technology|Materials, metallurgy B01D-053/62|B01D-053/80|B01D-2257/504|B01D-2258/0283|C04B-005/00|C04B-005/06 B01D-053/62|B01D-053/80|B01D-2257/504|B01D-2258/0283|C04B-005/00|C04B-005/06 B01D-053/62|B01D-053/80|C04B-005/00|C04B-005/06 B01D-053/62|B01D-053/80|C04B-005/00|C04B-005/06 PENDING (CN118993582)|PENDING ALIVE (CN118993582)|ALIVE (CN118993582)|LEGAL DETAILS FOR CN118993582|Actual or expected expiration date=2044-07-24|Legal state=ALIVE|Status=PENDING|Event publication date=2024-07-24|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202411000248|Application date=2024-07-24|Standardized application number=2024CN-1000248|Event publication date=2024-11-22|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN118993582|Publication stage code=A|Publication date=2024-11-22|Standardized publication number=CN118993582|Event publication date=2024-11-22|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-12-10|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN118993582)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTKmhmlj65l71fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000075319225&ekey=2037&xpn=CN118993582&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=1t2QNTYhf0HiffHJ3KV9xZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN118993582)|CN (CN118993582)|NAME=DONGFANG ELECTRIC GROUP DONGFANG BOILER CO. LTD. , COUNTRY=CN (CN118993582)|NAME=LIU SHIQUAN;CHENGDU JIUDING TIANYUAN INTELLECTUAL PROPERTY AGENCY CO. LTD. , REG=51214 (CN118993582)|NAME=WANG BO|NAME=HU SHILEI|NAME=LI NA|NAME=YANG HUAN|NAME=LIANG QUANXUN|NAME=DENG YI|NAME=ZHUANG YUANFA 0 1 Titre: (CN118993582)|System and method for capturing and mineralizing converter flue gas CO2 through steel slag-wastewater Résumé: (CN118993582)|The invention discloses a system and a method for capturing and mineralizing CO2 in converter flue gas by steel slag-wastewater. The method comprises the following steps: step (1), crushing steel slag and grinding into steel slag micro powder with the particle size of less than 150 microns; (2) the steel slag micro powder and the steel mill wastewater are simultaneously placed in mixing equipment for a Ca < 2 + > leaching reaction; (3) conveying the mixed steel slag slurry from which Ca < 2 + > is leached to a mineralization reactor, and meanwhile, introducing converter flue gas to carry out gas-liquid-solid three-phase mineralization reaction; and (4) carrying out solid-liquid separation on the mineralized slurry after the reaction is finished to obtain mineralized steel slag. Compared with a two-phase mineralization reaction, the method has the advantages that the carbon sequestration rate of the steel slag is increased, the mineralization rate of the steel slag is increased, green low-carbon cement can be prepared after the prepared steel slag is mixed with cured cement, the performance of the cement is better, the problems of discharge and recycling of wastes such as the steel slag, wastewater and waste gas are solved, waste discharge is reduced, and energy conservation and environmental protection are facilitated. 116 Abstract gpt-4o-mini no The focus is on capturing CO2 from flue gas using steel slag and wastewater, which falls under industrial processes rather than enhanced weathering or mineral carbonation aimed at carbon sequestration in natural environments.
117 CN202511559558 CN202511559558 CN121253236 117274553 CN121253236 A 2026-01-02 [CN121253236] 2025-10-29 2025-10-29 2026-01-02 (CN121253236)|2045-10-29 (CN121253236)|Buried soil water collecting system (CN121253236)|The invention provides a buried soil water collection system, and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance, a porous ceramic tube is buried in soil, a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube, and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action, so that the soil water is absorbed by the porous ceramic tube; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube, and the porous water absorption material can continuously adsorb and store the soil water. When the water storage amount in the porous water absorption material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorption material, so that the soil water stored in the porous water absorption material is extruded out, and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe, so that the soil water is centrally stored in the water storage container. Therefore, the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. LANZHOU UNIVERSITY|MICROCARBON LOW CARBON TECHNOLOGY (CN121253236)|LANZHOU UNIVERSITY ([CN])|Microcarbon (Guangzhou) Low Carbon Technology Co., Ltd. ZHANG JIETANG|LI XINGYUAN|GOU XIAOHUA (CN121253236)|ZHANG JIETANG|LI XINGYUAN|GOU XIAOHUA (CN121253236)|HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 41028 (CN121253236)|Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water.|It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled.|Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.|2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect;|Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.| (CN121253236)|1. A buried soil water collection system, comprising: A fixed bracket; The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.| (CN121253236)|The invention provides a buried soil water collecting system, which belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction and treatment, wherein a porous ceramic tube is buried in soil, a porous water absorbing material and an extrusion component for extruding the porous water absorbing material are arranged in the porous ceramic tube, under the capillary action, the soil water adsorbed in the soil is adsorbed and transferred to the porous water absorbing material through the micropore structure of the porous ceramic tube, and the porous water absorbing material can continuously adsorb and store the soil water.|The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.| (CN121253236)|POROUS CERAMIC TUBE(100,106)|SOIL WATER COLLECTION(100,35)|BURIED SOIL WATER COLLECTION(100,9)|SOIL MOISTURE DYNAMICS(62,2)|SALINE SOIL RECONSTRUCTION(60,1)|NONWOVEN FABRIC(55,6)|EXPERIMENTAL SIMULATION AUTHENTICITY(52,1)|BURIED SOIL WATER COLLECTING(51,19)|MOISTURE DYNAMICS(44,2)|POROUS WATER(40,47)|ENHANCING SILICATE MINERAL WEATHERING(39,1)|RESEARCH SCIENTIFICITY(37,1)|MULTIFUNCTIONAL SILICATE MINERAL CONDITIONER(33,4)|EXTRUDING POROUS WATER(32,4)|SALINE SOIL CARBON(31,1)|SIMULATION EXPERIMENT(31,1)|DRIVING ROD(30,31)|BURYING SOIL(30,2)|GROUND(29,28)|EXTRUSION COMPONENT(29,11)|SOIL SALINITY(29,1)|PULL ROPE(28,6)|RELIABLE WEATHERING REACTION(28,1)|REAL MIGRATION(27,1)|SOIL ENVIRONMENT(26,4)|EXTRUDE POROUS WATER(24,7)|CONTAMINATION(24,2)|MICROPORE(23,5)|LIQUID COLLECTION(22,8)|SOIL WATER(21,76)|MICROPORE STRUCTURE(21,6)|GROUND LAYER(21,4)|MINERAL CONDITIONING AGENT DEVELOPMENT(21,1)|SILICATE MINERAL CONDITIONER(20,4)|DRIVING EXTRUSION(20,3)|MINERAL CONDITIONING AGENT(20,1)|SLIDING HOLE(19,24)|PUSH PULL ROD(19,22)|DYNAMIC MOISTURE(19,1)|FILTER LAYER(18,15)|SALT MIGRATION DATA(18,1)|REAL SOIL WATER SAMPLE(17,5)|TUBE SECTION(16,24)|MICROPOROUS STRUCTURE(16,10)|TUBE WALL(16,6)|BLOCK SEDIMENT(16,2)|CAPILLARY ACTION(15,11)|SOIL WATER ADSORBING MEMBER(15,3)|OUTLET HOLE(15,2)|PRECIPITATION(15,1)|SALTY SOIL(15,1)|COLUMNAR SPONGE END(14,11)|CARBON FIXATION(14,9)|SOIL WATER SAMPLE(14,5)|SLIDING MEMBER(14,2)|WATER OUTLET(13,15)|FIXED BRACKET(13,13)|SOIL WATER ADSORPTION COMPONENT(13,10)|POROUS WATER COMPRESSION RATIO(12,5)|COLUMNAR SPONGE DIRECTION(12,3)|MECHANISM RESEARCH(12,3)|POROUS WATER ABSORPTION(12,2)|CERAMIC TUBE(12,1)|EFFECT EVALUATION(12,1)|PUSH PULL TUBE GLASS CERAMIC(12,1)|PRESSING PIECE(11,16)|ROCK(11,2)|SLIDING ROD DRIVING(11,2)|WATER STORAGE CONTAINER(10,16)|ELASTIC MEMBER(10,7)|PRESSING MEMBER DRIVING(10,1)|WATERTIGHT COMPACT STRUCTURE(10,1)|SOIL WATER EXTRUSION(9,5)|ACCURATE EXPERIMENTAL DATA(9,3)|SYMMETRICAL AXIS(9,3)|CONNECTING ROD(8,16)|PISTON ROD(8,10)|COIL SPRING(8,9)|POROUS STRUCTURE(8,9)|REPEATABLE EXPERIMENTAL DATA SUPPORT(8,3)|SURFACE CONTAMINATION(8,1)|FIXED SUPPORT(7,8)|LIQUID GUIDE TUBE(7,8)|COMPRESSION RATIO(7,7)|POROUS WATER POROUS STRUCTURE(7,6)|CHEMICAL COMPOSITION(7,4)|POROUS WATER ABSORPTION MATERIAL(7,4)|POROUS CERAMIC PIPE(7,3)|OUTER PERIPHERAL(6,6)|SLIDING GROOVE(6,6)|PISTON OUTER CIRCUMFERENTIAL SURFACE(6,3)|PRODUCT OPTIMIZATION(6,3)|EXTRUSION SUBASSEMBLY(6,2)|MINERAL DISSOLUTION REALITY(6,1)|PRODUCT DEVELOPMENT(6,1)|SALINE SOIL RECLAMATION(6,1)|PIPE SECTION(5,17)|PULLEY BLOCK(5,8)|WATER ABSORPTION MATERIAL(5,4)|COLUMN SPONGE(5,3)|PULLEY BRACKET(5,2)|CARBON FIXATION PROCESS DATA(5,1)|CHINESE SALINE ALKALI SOIL(5,1)|NONWOVEN FABRICS(5,1)|POTASSIUM MICROELEMENT(5,1)|PROCESS DATA(5,1)|SALINE ALKALI BARREN LAND(5,1)|WATER STORAGE(4,22)|OPEN END(4,10)|FIELD CONDITION(4,4)|MOISTURE DYNAMIC(4,2)|SALINIZED SOIL IMPROVEMENT(4,2)|UNCOMPRESSED(4,2)|AIRTIGHT COMPACT(4,1)|ECOLOGICAL SAFETY(4,1)|ERODE ELASTIC PIECE(4,1)|EXTENSIVE UTILIZATION(4,1)|WATERPROOF SEALING(4,1)|WEATHERING EXPERIMENT(4,1)|OUTER SIDE(3,7)|PIPE WALL(3,6)|MOVEABLE PULLEY(3,5)|CYLINDRICAL SPRING(3,2)|ELASTICITY(3,2)|INNER SIDEWALL(3,2)|SEALING PERFORMANCE ENHANCEMENT(3,2)|SLIDING SHAFT(3,2)|SLIDING SLOT(3,2)|AIRTIGHT SEALING FILM(3,1)|ATMOSPHERIC CO2 FIXATION(3,1)|BLOCKING SEDIMENT(3,1)|ELASTIC BUFFERING ACTION(3,1)|ENHANCING SILICATE MINERAL(3,1)|FINISH EXTRUSION(3,1)|SALT MIGRATION(3,1)|CENTRAL POSITION(2,4)|SPIRAL SPRING(2,4)|GROUND SECTION(2,3)|ABSORBENT COTTON(2,1)|ALKALI ION(2,1)|ARTIFICIALLY PREPARED LEACHING SOLUTION(2,1)|BICARBONATE(2,1)|COLUMNAR SPONGE COMPRESSION RATIO(2,1)|COLUMNAR SPONGE FLOW(2,1)|DRENCHING SOLUTION(2,1)|EVALUATION ERROR(2,1)|EXCHANGE REACTION NA(2,1)|EXTENSIVE TREATMENT(2,1)|ION MIGRATION(2,1)|KEY INDEX(2,1)|MICROENVIRONMENT(2,1)|OPENING END(2,1)|PIPE CAVITY(2,1)|SALINE ALKALI LAND(2,1)|STABLE PROMOTION(2,1)|SURFACE WATER SAMPLE(2,1)| (CN121253236)|1. A buried soil water collection system, comprising:| A fixed bracket; | The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; | the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; | The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; | a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and |The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.|2. The buried soil water collecting system according to claim 1, wherein the porous water absorbing material is a columnar sponge, an axial direction of the columnar sponge is parallel to an axial direction of the porous ceramic tube, and an outer peripheral surface of the columnar sponge is in contact with an inner side wall of the porous ceramic tube.|3. The buried soil water collection system according to claim 2, wherein the extrusion assembly comprises a first pressing member slidably disposed in the porous ceramic tube, a second pressing member slidably disposed in the porous ceramic tube, an elastic member for elastically pressing the second pressing member against the first pressing member, and a push-pull rod for driving the first pressing member to slide against the second pressing member, the first pressing member is disposed adjacent to the closed end of the porous ceramic tube, the first pressing member is abutted against the first end of the columnar sponge, the second pressing member is disposed adjacent to the open end of the porous ceramic tube, the first pressing member is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is disposed on the second pressing member, a second sliding hole for the rod to pass through is disposed on the columnar sponge, the first end of the push-pull rod extends into the porous ceramic tube via the open end of the push-pull ceramic tube, and the first end of the push-pull rod is sequentially connected to the first sliding member after passing through the first sliding hole and the second sliding member.|4. The buried soil water collecting system according to claim 3, wherein the elastic member is a coil spring accommodated in the porous ceramic tube, an opening end of the porous ceramic tube is provided with a holding cover for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover, the other end of the coil spring is held against the second holding member, and a third sliding hole for the push-pull rod to pass through is formed in the holding cover.|5. The system of claim 3, wherein the first pressing member comprises a first piston slidably disposed in the porous ceramic tube and a first pressing member connected to the first piston, wherein an outer circumferential surface of the first piston is in interference contact with an inner side wall of the porous ceramic tube, the first pressing member is in interference contact with a first end of the columnar sponge, and wherein the second pressing member comprises a second pressing member slidably disposed in the porous ceramic tube and connected to the second piston, wherein an outer circumferential surface of the second piston is in interference contact with an inner side wall of the porous ceramic tube, and wherein the second pressing member is in interference contact with a second end of the columnar sponge.|6. The buried soil water collecting system according to claim 5, wherein the porous ceramic tube comprises a first tube section and a second tube section which are integrally formed, wherein one end of the first tube section away from the second tube section is a closed end, one end of the second tube section away from the first tube section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on a tube wall of the first tube section, the first piston and the columnar sponge are positioned in the first tube section, the tube wall of the second tube section is of a gas-tight and water-tight compact structure, the second piston and the elastic element are positioned in the second tube section, and the water outlet is arranged on the tube wall of the second tube section.|7. A buried soil water collecting system according to claim 3, wherein a plurality of said soil water adsorbing members are provided in a plurality, said plurality of said soil water adsorbing members being arranged side by side and at intervals, each of said soil water adsorbing members being provided with one said pressing member, each of said pressing members being connected to said driving means.|8. The buried soil water collecting system according to claim 7, wherein the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding manner, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction of the sliding rod, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the central position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.|9. The buried soil water collecting system according to claim 8, wherein the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, a pull rope is wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with the corresponding piston rods, and the second end of the driving rod is connected with a central position of the connecting rod.|10. A buried soil water collecting system according to any one of claims 1 to 9 wherein said filter layer comprises at least one layer of non-woven fabric or silt filter screen. (CN121253236)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reclamation and treatment, and particularly relates to a buried soil water collection system.|BACKGROUND ART|[0002] China is a large country of saline-alkali soil, and the third country is the first 10 countries in the area of saline-alkali soil. The Chinese saline-alkali soil is distributed in 17 provinces including northwest, northeast, north China and coastal areas, the total area of the saline-alkali barren lands and the saline-alkali lands affecting the cultivated lands exceeds 5 hundred million mu, and the agricultural production and the ecological safety are seriously restricted. In order to respond to the requirements of comprehensive treatment and comprehensive utilization of saline-alkali soil with stable promotion, development of a multifunctional silicate mineral conditioner with functions of improving saline-alkali soil, supplementing trace elements and fixing carbon is needed. The conditioner relies on the technology of enhancing silicate mineral weathering, and releases Ca 2+、Mg2+ and other exchange reactions Na +、CO2- 3、HCO-3 through mineral weathering, so that the salt and alkali ions are reduced, and simultaneously, the microelements of potassium, phosphorus, magnesium, zinc, selenium and other nutrients are released, and the fixation of atmospheric CO2 is realized in the mineral weathering-carbonate precipitation process.|[0003] In the technical development process, a field-scale silicate mineral leaching weathering experiment is a key link for verifying mineral improvement effect and carbon sequestration potential. The weathering, ion migration and salt replacement processes of minerals in the soil take soil water as a main reaction medium, and the changes of cations, anions, dissolved inorganic carbon and other components in the soil water can directly reflect the weathering rate, the carbon fixation reaction process and the salt migration condition of the minerals. However, the prior art generally relies on manually formulating water or groundwater as a drenching solution, or employing surface runoff sampling instead of in situ soil water collection, which results in:| 1) The weathering reaction condition is distorted, namely the artificially prepared leaching solution cannot accurately reproduce the pH value, the ionic strength and the organic acid content of the soil in the microenvironment, and the reality of mineral dissolution and carbonate precipitation reaction is affected; | 2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect; | 3) The carbon fixation amount has distortion and deviation, namely, the key indexes such as Dissolved Inorganic Carbon (DIC) and bicarbonate (HCO 3 -) in the in-situ soil water are lacked, so that the evaluation error of the carbon fixation amount is large. |[0004] Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.|[0005] The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.|DISCLOSURE|Disclosure of Invention|[0006] Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.|[0007] In order to achieve the above purpose, the invention adopts the technical scheme that the buried soil water collecting system comprises:| A fixed bracket; | The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; | the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; | The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; | a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and |The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.|[0008] Further, the porous water absorbing material is a columnar sponge, the axial direction of the columnar sponge is parallel to the axial direction of the porous ceramic tube, and the outer peripheral surface of the columnar sponge is in contact with the inner side wall of the porous ceramic tube.|[0009] Further, the extrusion assembly comprises a first abutting part arranged in the porous ceramic tube in a sliding manner, a second abutting part arranged in the porous ceramic tube in a sliding manner, an elastic part for elastically abutting the second abutting part towards the first abutting part, and a push-pull rod for driving the first abutting part to slide towards the second abutting part, wherein the first abutting part is arranged close to the closed end of the porous ceramic tube, the first abutting part is abutted against the first end of the columnar sponge, the second abutting part is arranged close to the opening end of the porous ceramic tube, the first abutting part is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is formed in the second abutting part, a second sliding hole for the push-pull rod to pass through is formed in the columnar sponge, the first end of the rod stretches into the porous ceramic tube through the opening end of the porous ceramic tube, and is connected with the first abutting part after sequentially passing through the first sliding hole and the second hole, and the first abutting part is connected with the second driving device.|[0010] Further, the elastic piece is a spiral spring accommodated in the porous ceramic tube, an abutting cover for abutting against the spiral spring is arranged at the opening end of the porous ceramic tube, one end of the spiral spring abuts against and is fixed on the abutting cover, the other end of the spiral spring abuts against the second abutting piece, and a third sliding hole for the push-pull rod to pass through is formed in the abutting cover.|[0011] Further, the first pressing piece comprises a first piston arranged in the porous ceramic tube in a sliding mode and a first pressing piece connected with the first piston, the outer peripheral surface of the first piston is in interference contact with the inner side wall of the porous ceramic tube, the first pressing piece is in interference contact with the first end of the columnar sponge, the second pressing piece comprises a second pressing piece connected with the second piston in the porous ceramic tube in a sliding mode, the outer peripheral surface of the second piston is in interference contact with the inner side wall of the porous ceramic tube, and the second pressing piece is in interference contact with the second end of the columnar sponge.|[0012] Further, the porous ceramic pipe comprises a first pipe section and a second pipe section which are integrally formed, one end, away from the second pipe section, of the first pipe section is a closed end, one end, away from the first pipe section, of the second pipe section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on the pipe wall of the first pipe section, the first piston and the columnar sponge are located in the first pipe section, the pipe wall of the second pipe section is of an airtight and waterproof compact structure, the second piston and the elastic piece are located in the second pipe section, and the water outlet is formed in the pipe wall of the second pipe section.|[0013] Further, the quantity of soil water adsorption components sets up to a plurality of, and is a plurality of soil water adsorption components just interval arrangement side by side, every soil water adsorption components is supporting to be set up one extrusion subassembly, every extrusion subassembly with drive arrangement links to each other.|[0014] Further, the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding mode, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the centering position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.|[0015] Further, the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, pull ropes are wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with corresponding piston rods, and the second end of the driving rod is connected with a centering position of the connecting rod.|[0016] Further, the filter layer comprises at least one layer of non-woven fabrics or silt filter screens.|[0017] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:| According to the buried soil water collecting system provided by the embodiment of the invention, the porous ceramic pipe with the pipe wall having the micropore structure is buried in soil, the porous ceramic pipe is internally provided with the porous water absorbing material capable of absorbing and storing soil water and the extrusion component capable of extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic pipe under the capillary action, and is absorbed and transmitted to the porous water absorbing material through the micropore structure of the porous ceramic pipe, so that the porous water absorbing material can continuously absorb and store the soil water. And when the water storage amount in the porous water absorbing material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorbing material, so that the soil water stored in the porous water absorbing material is extruded, and the extruded soil water is drained to the water storage container through the water outlet holes and the liquid guide tube on the porous ceramic tube, so that the soil water is stored in the water storage container in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation. |DRAWINGS DESCRIPTION|[0018] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.|[0019] FIG. 1 is a schematic perspective view of a buried soil water collection system according to the present invention;| FIG. 2 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; | FIG. 3 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; | FIG. 4 is a schematic view of a buried soil water collection system according to the present invention buried in soil; | FIG. 5 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in an uncompressed state according to the present invention; | FIG. 6 is a cross-sectional view of the soil water adsorbing assembly and squeeze assembly of the present invention in an uncompressed state; | FIG. 7 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in a squeezed state according to the present invention; | FIG. 8 is a cross-sectional view of the soil water adsorbing assembly and the squeezing assembly according to the present invention in a squeezed state; | fig. 9 is an exploded view of a soil water adsorbing assembly and a squeezing assembly according to the present invention. |[0020] Wherein, each reference sign in the figure:| 1-a fixed bracket, 11-a sliding groove; | 2-a soil water adsorption component, 21-a porous ceramic tube, 211-a first tube section, 212-a second tube section, 213-a water outlet hole, 22-a porous water absorbing material, 221-a second sliding hole, 23-a supporting cover and 231-a third sliding hole; | 3-extrusion assembly, 31-first pressing piece, 311-first piston, 312-first pressing piece, 32-second pressing piece, 321-second piston, 322-second pressing piece, 323-first sliding hole, 33-elastic piece and 34-push-pull rod; | 4-driving device, 41-sliding rod, 42-driving rod, 43-cylinder, 431-piston rod, 44-pulley block, 441-fixed pulley, 442-movable pulley, 45-pull rope, 451-vertical section, 46-first pulley bracket, 47-second pulley bracket, 48-sliding chute or bar-shaped sliding hole and 49-connecting rod; | a 5-liquid collecting system, a 51-water storage container, a 52-liquid guiding tube; | 6-soil profile and 7-sliding shaft. |INVENTION MODE|Detailed Description|[0021] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0022] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," "third," and "fourth" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first", "a second", "a third", and "a fourth" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.|[0023] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.|[0024] Referring to fig. 1 to 9, a description will be given of a buried soil water collecting system according to an embodiment of the present invention. Referring to fig. 1, 2 and 3 in combination, the buried soil water collecting system according to the embodiment of the present invention includes a fixing bracket 1, a soil water adsorbing assembly 2, an extruding assembly 3, a driving device 4, a liquid collecting system 5 and a filtering layer, wherein the fixing bracket 1 is used for fixing on one side of a soil profile 6, and is mainly used for supporting and fixing the whole buried soil water collecting system. The soil water adsorption assembly 2 is capable of adsorbing and storing soil water in soil by capillary action, the soil water adsorption assembly 2 comprises a porous ceramic tube 21 for burying the soil and a porous water absorbing material 22 arranged in the porous ceramic tube 21, a first end of the porous ceramic tube 21 is a closed end, the closed end of the porous ceramic tube 21 is in a conical structure so as to facilitate the insertion of the porous ceramic tube 21 into the soil, and a second end of the porous ceramic tube 21 is an open end. The position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is detachably connected or fixedly connected with the fixed support 1, and the position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is provided with a water outlet hole 213, and the water outlet hole 213 is communicated with the inner cavity of the porous ceramic tube 21. The porous ceramic tube 21 has a microporous structure on the wall, which can adsorb and transfer soil water in soil to the porous water absorbing material 22 by capillary action, the porous water absorbing material 22 has a continuous and mutually penetrating porous structure inside, and the porous water absorbing material 22 can adsorb and store a certain volume of soil water. The porous ceramic tube 21 has a cylindrical structure, and can ensure a maximum area of contact with the soil. Meanwhile, the porous water absorbing material 22 has a cylindrical structure, and can ensure contact with the inner tube wall of the porous ceramic tube 21 at a maximum area.|[0025] The extrusion component 3 is movably arranged in the porous ceramic tube 21, and the extrusion component 3 is used for extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22, so that soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water flows out of the porous ceramic tube 21 through the water outlet holes 213 on the porous ceramic tube 21. The driving device 4 is arranged on the fixed bracket 1, the driving device 4 is connected with the extrusion assembly 3, and the driving device 4 is used for driving the extrusion assembly 3 to extrude the porous water absorbing material 22 according to a preset program or periodically, so that soil water stored in a continuous porous structure of the porous water absorbing material 22 is extruded. The liquid collecting system 5 includes a water storage container 51 for collecting soil water and a liquid guide tube 52 connecting the water storage container 51 with the water outlet 213, and the soil water flowing out through the water outlet 213 can be concentrated and stored in the water storage container 51 by drainage of the liquid guide tube 52. The filter layer wraps the outer side of the porous ceramic tube 21, and can allow soil water to permeate into the microporous structure of the porous ceramic tube 21, and meanwhile, the filter layer can block sediment in soil on the outer side of the porous ceramic tube 21, so that sediment in soil is blocked to block the microporous structure of the porous ceramic tube 21.|[0026] Referring to fig. 4, a vertical section is excavated on one side of the soil to be taken, a porous ceramic tube 21 of a soil water adsorption component 2 is transversely inserted or buried into the soil through a soil section 6, a fixing support 1 is fixed on one side of the soil section 6, so that the porous ceramic tube 21 of the soil water adsorption component 2 cannot relatively displace with the soil, and a waterproof and airtight sealing film is paved on the soil surface and the soil section 6, wherein the sealing film can be, but is not limited to, a plastic film. In this way, the water (soil water) absorbed in the soil can permeate the filter layer, under the capillary action, the water is absorbed by the micropore structure of the porous ceramic tube 21 and is transmitted to the porous water absorbing material 22, the porous water absorbing material 22 continuously absorbs the soil water and continuously stores the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22, when the water storage capacity in the porous water absorbing material 22 reaches a certain value, the water storage capacity in the porous water absorbing material 22 can transmit a signal to the controller through the humidity sensor and/or the water content sensor, the controller controls the driving device 4 to work according to a preset program after receiving the signal, the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, and the soil water is concentrated and stored in the water storage container 51. After the soil water in the porous water absorbing material 22 is fully extruded, the controller controls the driving device 4 to stop working, at this time, the extrusion assembly 3 finishes the extrusion action on the porous water absorbing material 22, the porous water absorbing material 22 can recover the original state, continuously absorb the soil water again, and continuously store the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22 until the water storage amount in the porous water absorbing material 22 reaches a certain value, the controller can transmit signals to the controller through the humidity sensor and/or the water content sensor, after receiving the signals, the controller controls the driving device 4 to work according to a preset program, and the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded.|[0027] Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water. Until the water storage amount in the porous water absorbing material 22 is sufficient, the squeezing component 3 is driven by the driving device 4 to squeeze the porous water absorbing material 22, so that the soil water stored in the porous water absorbing material 22 is squeezed out, and the squeezed soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, so that the soil water is stored in the water storage container 51 in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation.|[0028] Referring to fig. 6, 8 and 9 in combination, in some embodiments, the porous water absorbing material 22 is a cylindrical sponge, the axial direction of the cylindrical sponge is parallel to the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the cylindrical sponge is in contact with the inner side wall of the porous ceramic tube 21. In this embodiment, the porous water absorbing material 22 is preferably a sponge with good water absorbing and storing properties, and the sponge is arranged in the porous ceramic tube 21 in a columnar shape, so that the axial direction of the columnar sponge is consistent with the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the columnar sponge is contacted with the inner side wall of the porous ceramic tube 21, thereby ensuring that the columnar sponge is contacted with the inner tube wall of the porous ceramic tube 21 in the largest area, and improving the adsorption and collection effects of soil water. In addition, the sponge is arranged in the porous ceramic tube 21 in a columnar shape, and is compressed from the axial direction of the columnar sponge through the extrusion component 3, so that on one hand, the compression ratio of the columnar sponge can be increased to fully extrude soil water in the columnar sponge, and the adsorption and collection efficiency of the soil water can be further improved, and on the other hand, when the extrusion component 3 finishes extrusion action on the columnar sponge, the columnar sponge is favorable for quickly recovering the original state, and then the soil water can be better adsorbed and stored later. The porous absorbent material 22 may be, but is not limited to, a sponge, and the porous absorbent material 22 may also be a porous material having a certain compression ratio, such as absorbent cotton, nonwoven fabric, or the like.|[0029] Referring to fig. 6, 8 and 9, in some embodiments, the pressing assembly 3 includes a first pressing member 31 slidably disposed in the porous ceramic tube 21, a second pressing member 32 slidably disposed in the porous ceramic tube 21, an elastic member 33 for elastically pressing the second pressing member 32 toward the first pressing member 31, and a push-pull rod 34 for driving the first pressing member 31 to slide toward the second pressing member 32, wherein the first pressing member 31 is disposed adjacent to the closed end of the porous ceramic tube 21, the first pressing member 31 abuts against a first end of the columnar sponge, the second pressing member 32 is disposed adjacent to the open end of the porous ceramic tube 21, the first pressing member 31 abuts against a second end of the columnar sponge, a first sliding hole 323 for the push-pull rod 34 to pass through is disposed on the second pressing member 32, a second sliding hole 221 for the push-pull rod 34 to pass through is disposed on the columnar sponge, the first end of the rod 34 extends into the porous ceramic tube 21 through the open end of the porous ceramic tube 21, and is connected to the first sliding hole 323 and the second sliding hole 221 after sequentially passing through the first sliding hole and the second sliding hole 221, and the second pressing member 31 abuts against a second end of the columnar sponge, and the second end of the rod 34 is connected to the driving device 4. In this embodiment, the driving device 4 pulls the push-pull rod 34 towards the open end of the porous ceramic tube 21, the push-pull rod 34 drives the first pressing member 31 to move towards the second pressing member 32, and as the distance between the first pressing member 31 and the second pressing member 32 gradually decreases, the columnar sponge between the first pressing member 31 and the second pressing member 32 is continuously compressed, and the soil water in the columnar sponge is also continuously extruded in the compression process. In the process of pressing the columnar sponge by the first pressing piece 31 and the second pressing piece 32, the second pressing piece 32 is elastically pressed against the first pressing piece 31 by the elastic piece 33, so that soil water in the columnar sponge is slowly released under the elastic buffering action of the elastic piece 33, the columnar sponge is prevented from being excessively compressed by the first pressing piece 31 and the second pressing piece 32 instantly, the pressure in the porous ceramic tube 21 is instantly increased, the soil water can leak through the micropore structure of the porous ceramic, and the pH value and the ion concentration in the soil water can be changed. Because be equipped with the second slide hole 221 that supplies push-and-pull rod 34 to pass on the column sponge, the column sponge passes through second slide hole 221 cover and locates on the push-and-pull rod 34, in the in-process of first pressure piece 31 and the extrusion of second pressure piece 32 column sponge, not only can effectively avoid the column sponge that axial length is longer to take place distortion, can be favorable to the column sponge later stage to resume original state fast moreover. It should be noted that, a sealing ring is disposed between the push-pull rod 34 and the first sliding hole 323 to enhance the sealing performance of the sliding contact between the push-pull rod 34 and the first sliding hole 323. In addition, locate the column sponge between first pressure piece 31 and the second pressure piece 32 to push up the elasticity of second pressure piece 32 towards first pressure piece 31 through elastic component 33, on the one hand be favorable to high efficiency with the soil water extrusion in the column sponge, on the other hand can push back the column sponge to the position that adsorbs the soil water through the action of pushing up of elastic component 33 fast through the second pressure piece 32.|[0030] Referring to fig. 5, 8 and 9 in combination, in some embodiments, the elastic member 33 is a coil spring accommodated in the porous ceramic tube 21, the open end of the porous ceramic tube 21 is provided with a holding cover 23 for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover 23, the other end of the coil spring is held against the second holding member 32, the holding cover 23 is provided with a third sliding hole 231 through which the push-pull rod 34 passes, and a sealing ring is disposed between the push-pull rod 34 and the third sliding hole 231 to enhance the sealing performance of sliding contact between the push-pull rod 34 and the third sliding hole 231. It should be noted that the holding cover 23 may be, but not limited to, connected to the open end of the porous ceramic tube 21 by a threaded connection, and the elastic member 33 may be, but not limited to, a coil spring.|[0031] Referring to fig. 6, 8 and 9, in some embodiments, the first pressing member 31 includes a first piston 311 slidably disposed in the porous ceramic tube 21 and a first pressing member 312 connected to the first piston 311, the outer peripheral surface of the first piston 311 is in interference contact with the inner sidewall of the porous ceramic tube 21, the first pressing member 312 abuts against the first end of the cylindrical sponge, the first piston 311 is a rubber member or a silicone member having elasticity, the first pressing member 312 is a hard metal sheet or a plastic sheet, and a supporting and reinforcing effect is formed on the first piston 311 by the first pressing member 312, so as to prevent the first pressing member 31 from deforming during the process of pressing the cylindrical spring. Similarly, the second pressing member 32 includes a second pressing member 322 slidably disposed in the porous ceramic tube 21 and connected to the second piston 321, where the outer circumferential surface of the second piston 321 is in interference contact with the inner sidewall of the porous ceramic tube 21, the second pressing member 322 abuts against the second end of the cylindrical sponge, the second piston 321 is a rubber member or a silica gel member having elasticity, and the second pressing member 322 is a hard metal sheet or a plastic sheet, and forms a supporting and reinforcing effect on the second piston 321 by the second pressing member 322, so as to prevent the deformation of the first pressing member 31 in the process of pressing the cylindrical spring.|[0032] Referring to fig. 7, 8 and 9 in combination, in some embodiments, the porous ceramic tube 21 includes a first tube section 211 and a second tube section 212 that are integrally formed, one end of the first tube section 211 away from the second tube section 212 is a closed end, one end of the second tube section 212 away from the first tube section 211 is an open end, a microporous structure capable of adsorbing and transmitting soil water is provided on a tube wall of the first tube section 211, the first piston 311 and the columnar sponge are located in the first tube section 211, and the soil water can be adsorbed and transmitted to the columnar sponge in the first tube section 211 by capillary action of the microporous structure. Meanwhile, the pipe wall of the second pipe section 212 is of a dense structure which is airtight and watertight, and the second piston 321 and the elastic piece 33 are located in the second pipe section 212, so that the elastic piece 33 in the second pipe section 212 cannot pollute soil water, and meanwhile, the soil water cannot flow into the second pipe section 212 to erode the elastic piece 33. It should be noted that, when the first pressing member 31 drives the columnar sponge into the second pipe section 212, the elastic member 33 is in a compressed state, and the elastic member 33 can elastically press the second pressing member 32 against the first pressing member 31, so that the second pressing member 32 cooperates with the first pressing member 31 to compress the columnar sponge into the sealed second pipe cavity, and the soil water extruded from the columnar sponge flows out through the water outlet 213 on the pipe wall of the second pipe section 212. In addition, when the second pressing member 32 compresses the columnar sponge in the sealed second lumen in cooperation with the first pressing member 31, the pressure in the second tube section 212 can be increased, so that the soil water in the second tube section 212 is pressed out, and the collection efficiency of the soil water can be accelerated.|[0033] Referring to fig. 1, 2 and 3, in some embodiments, in order to collect soil water more quickly and efficiently, a plurality of soil water adsorbing assemblies 2 are arranged, and a plurality of soil water adsorbing assemblies 2 are arranged side by side and at intervals, and each soil water adsorbing assembly 2 is provided with a squeezing assembly 3 in a matching manner, and each squeezing assembly 3 is connected with a driving device 4.|[0034] Referring to fig. 1, 2 and 3, in some embodiments, the driving device 4 includes a sliding rod 41 with two ends slidably disposed on the fixed support 1, a driving rod 42 for driving the sliding rod 41 to move along the axial direction of the push-pull rod 34, and an air cylinder 43 for driving the driving rod 42 to move along the axial direction, the fixed support 1 is provided with a sliding groove 11, and two ends of the sliding rod 41 are slidably inserted into the sliding groove 11. The axial direction of the sliding rod 41 is perpendicular to the axial direction of the sliding rod 34, the second end of the sliding rod 34 is connected with the sliding rod 41, the axial direction of the driving rod 42 is parallel to the axial direction of the sliding rod 34, the first end of the driving rod 42 is connected with the central position of the sliding rod 34, and the second end of the driving rod 42 is connected with a piston rod 431 of the air cylinder 43. In this embodiment, the push-pull rod 34 is driven to axially move by the telescopic movement of the piston rod 431 of the air cylinder 43, so that the driving rod 42 can be driven to axially move along the driving rod 42 by the push-pull rod 34, the sliding rod 41 further drives the push-pull rod 34 to axially move, and the push-pull rod 34 drives the first pressing member 31 to reciprocate along the axial direction of the porous ceramic tube 21, so that the columnar sponge can be pressed by the first pressing member 31 and the second pressing member 32. It should be noted that, the fixed bracket 1 is provided with a sliding slot, two ends of the sliding rod 41 are respectively disposed in the corresponding sliding slots, the fixed bracket 1 is further provided with a fourth sliding hole, and the driving shaft is slidably inserted into the fourth sliding hole.|[0035] Referring to fig. 1,2 and 3 in combination, in some embodiments, in order to enhance the stability of the movement of the push-pull rod 34 driven by the driving device 4 and to maintain the high precision operation of the push-pull rod 34, the number of the air cylinders 43 is two, the piston rods 431 of the two air cylinders 43 are symmetrically distributed with the central axis of the driving rod 42 as a symmetrical axis, the driving device 4 further comprises a connecting rod 49 axially perpendicular to the axial direction of the push-pull rod 34 and two pulley blocks 44 symmetrically arranged at two sides of the driving rod 42, each pulley block 44 is wound with a pull rope 45, the axial direction of the vertical section 451 of each pull rope 45 is parallel to the axial direction of the push-pull rod 34, one pull rope 45 connects the first end of the sliding rod 41 with the first end of the connecting rod 49, the other pull rope 45 connects the second end of the sliding rod 41 with the second end of the connecting rod 49, and the two ends of the connecting rod 49 are respectively connected with the corresponding piston rods 431, and the second end of the driving rod 42 is connected with the central position of the connecting rod 49. It should be noted that, each pulley block 44 includes at least one fixed pulley 441 and at least one movable pulley 442, the fixed pulley 441 is rotatably disposed on the fixed bracket 1 through the first pulley bracket 46, the first pulley bracket 46 is fixedly connected with the fixed bracket 1, the movable pulley 442 is rotatably disposed on the fixed bracket 1 through the second pulley bracket 47, and the second pulley bracket 47 is fixedly connected with the fixed bracket 1. Specifically, the fixed support 1 is provided with a second pulley support 47, the second pulley support 47 is provided with a sliding groove or a bar-shaped sliding hole 48 capable of guiding the movable pulley 442 to slide along the axial direction of the driving rod 42, and two sections of sliding shafts 7 respectively inserted into the sliding groove or the bar-shaped sliding hole 48, and the movable pulley 442 is slidably arranged on the guiding support 48 through a sliding matching structure of the sliding shafts 7 and the sliding groove or the bar-shaped sliding hole 48.|[0036] It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled. Of course, the filter layer may also include at least one layer of sediment filter screen, and the filter layer may also be in other structural forms capable of blocking sediment outside the filter layer. It should be noted that the filter layer includes at least one layer of non-woven fabric or silt filter screen, which means that the filter layer wrapped on the outer side of the porous ceramic tube 21 may be a layer structure or a multi-layer structure, and is determined according to the filtering effects of different filtering materials and structures.|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention. (CN121253236)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reclamation and treatment, and particularly relates to a buried soil water collection system.|BACKGROUND ART|[0002] China is a large country of saline-alkali soil, and the third country is the first 10 countries in the area of saline-alkali soil. The Chinese saline-alkali soil is distributed in 17 provinces including northwest, northeast, north China and coastal areas, the total area of the saline-alkali barren lands and the saline-alkali lands affecting the cultivated lands exceeds 5 hundred million mu, and the agricultural production and the ecological safety are seriously restricted. In order to respond to the requirements of comprehensive treatment and comprehensive utilization of saline-alkali soil with stable promotion, development of a multifunctional silicate mineral conditioner with functions of improving saline-alkali soil, supplementing trace elements and fixing carbon is needed. The conditioner relies on the technology of enhancing silicate mineral weathering, and releases Ca 2+、Mg2+ and other exchange reactions Na +、CO2- 3、HCO-3 through mineral weathering, so that the salt and alkali ions are reduced, and simultaneously, the microelements of potassium, phosphorus, magnesium, zinc, selenium and other nutrients are released, and the fixation of atmospheric CO2 is realized in the mineral weathering-carbonate precipitation process.|[0003] In the technical development process, a field-scale silicate mineral leaching weathering experiment is a key link for verifying mineral improvement effect and carbon sequestration potential. The weathering, ion migration and salt replacement processes of minerals in the soil take soil water as a main reaction medium, and the changes of cations, anions, dissolved inorganic carbon and other components in the soil water can directly reflect the weathering rate, the carbon fixation reaction process and the salt migration condition of the minerals. However, the prior art generally relies on manually formulating water or groundwater as a drenching solution, or employing surface runoff sampling instead of in situ soil water collection, which results in:| 1) The weathering reaction condition is distorted, namely the artificially prepared leaching solution cannot accurately reproduce the pH value, the ionic strength and the organic acid content of the soil in the microenvironment, and the reality of mineral dissolution and carbonate precipitation reaction is affected; | 2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect; | 3) The carbon fixation amount has distortion and deviation, namely, the key indexes such as Dissolved Inorganic Carbon (DIC) and bicarbonate (HCO 3 -) in the in-situ soil water are lacked, so that the evaluation error of the carbon fixation amount is large. |[0004] Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.|[0005] The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.|DISCLOSURE|Disclosure of Invention|[0006] Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.|[0007] In order to achieve the above purpose, the invention adopts the technical scheme that the buried soil water collecting system comprises:| A fixed bracket; | The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; | the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; | The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; | a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and |The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.|[0008] Further, the porous water absorbing material is a columnar sponge, the axial direction of the columnar sponge is parallel to the axial direction of the porous ceramic tube, and the outer peripheral surface of the columnar sponge is in contact with the inner side wall of the porous ceramic tube.|[0009] Further, the extrusion assembly comprises a first abutting part arranged in the porous ceramic tube in a sliding manner, a second abutting part arranged in the porous ceramic tube in a sliding manner, an elastic part for elastically abutting the second abutting part towards the first abutting part, and a push-pull rod for driving the first abutting part to slide towards the second abutting part, wherein the first abutting part is arranged close to the closed end of the porous ceramic tube, the first abutting part is abutted against the first end of the columnar sponge, the second abutting part is arranged close to the opening end of the porous ceramic tube, the first abutting part is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is formed in the second abutting part, a second sliding hole for the push-pull rod to pass through is formed in the columnar sponge, the first end of the rod stretches into the porous ceramic tube through the opening end of the porous ceramic tube, and is connected with the first abutting part after sequentially passing through the first sliding hole and the second hole, and the first abutting part is connected with the second driving device.|[0010] Further, the elastic piece is a spiral spring accommodated in the porous ceramic tube, an abutting cover for abutting against the spiral spring is arranged at the opening end of the porous ceramic tube, one end of the spiral spring abuts against and is fixed on the abutting cover, the other end of the spiral spring abuts against the second abutting piece, and a third sliding hole for the push-pull rod to pass through is formed in the abutting cover.|[0011] Further, the first pressing piece comprises a first piston arranged in the porous ceramic tube in a sliding mode and a first pressing piece connected with the first piston, the outer peripheral surface of the first piston is in interference contact with the inner side wall of the porous ceramic tube, the first pressing piece is in interference contact with the first end of the columnar sponge, the second pressing piece comprises a second pressing piece connected with the second piston in the porous ceramic tube in a sliding mode, the outer peripheral surface of the second piston is in interference contact with the inner side wall of the porous ceramic tube, and the second pressing piece is in interference contact with the second end of the columnar sponge.|[0012] Further, the porous ceramic pipe comprises a first pipe section and a second pipe section which are integrally formed, one end, away from the second pipe section, of the first pipe section is a closed end, one end, away from the first pipe section, of the second pipe section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on the pipe wall of the first pipe section, the first piston and the columnar sponge are located in the first pipe section, the pipe wall of the second pipe section is of an airtight and waterproof compact structure, the second piston and the elastic piece are located in the second pipe section, and the water outlet is formed in the pipe wall of the second pipe section.|[0013] Further, the quantity of soil water adsorption components sets up to a plurality of, and is a plurality of soil water adsorption components just interval arrangement side by side, every soil water adsorption components is supporting to be set up one extrusion subassembly, every extrusion subassembly with drive arrangement links to each other.|[0014] Further, the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding mode, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the centering position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.|[0015] Further, the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, pull ropes are wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with corresponding piston rods, and the second end of the driving rod is connected with a centering position of the connecting rod.|[0016] Further, the filter layer comprises at least one layer of non-woven fabrics or silt filter screens.|[0017] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:| According to the buried soil water collecting system provided by the embodiment of the invention, the porous ceramic pipe with the pipe wall having the micropore structure is buried in soil, the porous ceramic pipe is internally provided with the porous water absorbing material capable of absorbing and storing soil water and the extrusion component capable of extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic pipe under the capillary action, and is absorbed and transmitted to the porous water absorbing material through the micropore structure of the porous ceramic pipe, so that the porous water absorbing material can continuously absorb and store the soil water. And when the water storage amount in the porous water absorbing material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorbing material, so that the soil water stored in the porous water absorbing material is extruded, and the extruded soil water is drained to the water storage container through the water outlet holes and the liquid guide tube on the porous ceramic tube, so that the soil water is stored in the water storage container in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation. |DRAWINGS DESCRIPTION|[0018] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.|[0019] FIG. 1 is a schematic perspective view of a buried soil water collection system according to the present invention;| FIG. 2 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; | FIG. 3 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; | FIG. 4 is a schematic view of a buried soil water collection system according to the present invention buried in soil; | FIG. 5 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in an uncompressed state according to the present invention; | FIG. 6 is a cross-sectional view of the soil water adsorbing assembly and squeeze assembly of the present invention in an uncompressed state; | FIG. 7 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in a squeezed state according to the present invention; | FIG. 8 is a cross-sectional view of the soil water adsorbing assembly and the squeezing assembly according to the present invention in a squeezed state; | fig. 9 is an exploded view of a soil water adsorbing assembly and a squeezing assembly according to the present invention. |[0020] Wherein, each reference sign in the figure:| 1-a fixed bracket, 11-a sliding groove; | 2-a soil water adsorption component, 21-a porous ceramic tube, 211-a first tube section, 212-a second tube section, 213-a water outlet hole, 22-a porous water absorbing material, 221-a second sliding hole, 23-a supporting cover and 231-a third sliding hole; | 3-extrusion assembly, 31-first pressing piece, 311-first piston, 312-first pressing piece, 32-second pressing piece, 321-second piston, 322-second pressing piece, 323-first sliding hole, 33-elastic piece and 34-push-pull rod; | 4-driving device, 41-sliding rod, 42-driving rod, 43-cylinder, 431-piston rod, 44-pulley block, 441-fixed pulley, 442-movable pulley, 45-pull rope, 451-vertical section, 46-first pulley bracket, 47-second pulley bracket, 48-sliding chute or bar-shaped sliding hole and 49-connecting rod; | a 5-liquid collecting system, a 51-water storage container, a 52-liquid guiding tube; | 6-soil profile and 7-sliding shaft. |INVENTION MODE|Detailed Description|[0021] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.|[0022] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," "third," and "fourth" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first", "a second", "a third", and "a fourth" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.|[0023] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.|[0024] Referring to fig. 1 to 9, a description will be given of a buried soil water collecting system according to an embodiment of the present invention. Referring to fig. 1, 2 and 3 in combination, the buried soil water collecting system according to the embodiment of the present invention includes a fixing bracket 1, a soil water adsorbing assembly 2, an extruding assembly 3, a driving device 4, a liquid collecting system 5 and a filtering layer, wherein the fixing bracket 1 is used for fixing on one side of a soil profile 6, and is mainly used for supporting and fixing the whole buried soil water collecting system. The soil water adsorption assembly 2 is capable of adsorbing and storing soil water in soil by capillary action, the soil water adsorption assembly 2 comprises a porous ceramic tube 21 for burying the soil and a porous water absorbing material 22 arranged in the porous ceramic tube 21, a first end of the porous ceramic tube 21 is a closed end, the closed end of the porous ceramic tube 21 is in a conical structure so as to facilitate the insertion of the porous ceramic tube 21 into the soil, and a second end of the porous ceramic tube 21 is an open end. The position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is detachably connected or fixedly connected with the fixed support 1, and the position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is provided with a water outlet hole 213, and the water outlet hole 213 is communicated with the inner cavity of the porous ceramic tube 21. The porous ceramic tube 21 has a microporous structure on the wall, which can adsorb and transfer soil water in soil to the porous water absorbing material 22 by capillary action, the porous water absorbing material 22 has a continuous and mutually penetrating porous structure inside, and the porous water absorbing material 22 can adsorb and store a certain volume of soil water. The porous ceramic tube 21 has a cylindrical structure, and can ensure a maximum area of contact with the soil. Meanwhile, the porous water absorbing material 22 has a cylindrical structure, and can ensure contact with the inner tube wall of the porous ceramic tube 21 at a maximum area.|[0025] The extrusion component 3 is movably arranged in the porous ceramic tube 21, and the extrusion component 3 is used for extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22, so that soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water flows out of the porous ceramic tube 21 through the water outlet holes 213 on the porous ceramic tube 21. The driving device 4 is arranged on the fixed bracket 1, the driving device 4 is connected with the extrusion assembly 3, and the driving device 4 is used for driving the extrusion assembly 3 to extrude the porous water absorbing material 22 according to a preset program or periodically, so that soil water stored in a continuous porous structure of the porous water absorbing material 22 is extruded. The liquid collecting system 5 includes a water storage container 51 for collecting soil water and a liquid guide tube 52 connecting the water storage container 51 with the water outlet 213, and the soil water flowing out through the water outlet 213 can be concentrated and stored in the water storage container 51 by drainage of the liquid guide tube 52. The filter layer wraps the outer side of the porous ceramic tube 21, and can allow soil water to permeate into the microporous structure of the porous ceramic tube 21, and meanwhile, the filter layer can block sediment in soil on the outer side of the porous ceramic tube 21, so that sediment in soil is blocked to block the microporous structure of the porous ceramic tube 21.|[0026] Referring to fig. 4, a vertical section is excavated on one side of the soil to be taken, a porous ceramic tube 21 of a soil water adsorption component 2 is transversely inserted or buried into the soil through a soil section 6, a fixing support 1 is fixed on one side of the soil section 6, so that the porous ceramic tube 21 of the soil water adsorption component 2 cannot relatively displace with the soil, and a waterproof and airtight sealing film is paved on the soil surface and the soil section 6, wherein the sealing film can be, but is not limited to, a plastic film. In this way, the water (soil water) absorbed in the soil can permeate the filter layer, under the capillary action, the water is absorbed by the micropore structure of the porous ceramic tube 21 and is transmitted to the porous water absorbing material 22, the porous water absorbing material 22 continuously absorbs the soil water and continuously stores the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22, when the water storage capacity in the porous water absorbing material 22 reaches a certain value, the water storage capacity in the porous water absorbing material 22 can transmit a signal to the controller through the humidity sensor and/or the water content sensor, the controller controls the driving device 4 to work according to a preset program after receiving the signal, the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, and the soil water is concentrated and stored in the water storage container 51. After the soil water in the porous water absorbing material 22 is fully extruded, the controller controls the driving device 4 to stop working, at this time, the extrusion assembly 3 finishes the extrusion action on the porous water absorbing material 22, the porous water absorbing material 22 can recover the original state, continuously absorb the soil water again, and continuously store the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22 until the water storage amount in the porous water absorbing material 22 reaches a certain value, the controller can transmit signals to the controller through the humidity sensor and/or the water content sensor, after receiving the signals, the controller controls the driving device 4 to work according to a preset program, and the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded.|[0027] Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water. Until the water storage amount in the porous water absorbing material 22 is sufficient, the squeezing component 3 is driven by the driving device 4 to squeeze the porous water absorbing material 22, so that the soil water stored in the porous water absorbing material 22 is squeezed out, and the squeezed soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, so that the soil water is stored in the water storage container 51 in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation.|[0028] Referring to fig. 6, 8 and 9 in combination, in some embodiments, the porous water absorbing material 22 is a cylindrical sponge, the axial direction of the cylindrical sponge is parallel to the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the cylindrical sponge is in contact with the inner side wall of the porous ceramic tube 21. In this embodiment, the porous water absorbing material 22 is preferably a sponge with good water absorbing and storing properties, and the sponge is arranged in the porous ceramic tube 21 in a columnar shape, so that the axial direction of the columnar sponge is consistent with the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the columnar sponge is contacted with the inner side wall of the porous ceramic tube 21, thereby ensuring that the columnar sponge is contacted with the inner tube wall of the porous ceramic tube 21 in the largest area, and improving the adsorption and collection effects of soil water. In addition, the sponge is arranged in the porous ceramic tube 21 in a columnar shape, and is compressed from the axial direction of the columnar sponge through the extrusion component 3, so that on one hand, the compression ratio of the columnar sponge can be increased to fully extrude soil water in the columnar sponge, and the adsorption and collection efficiency of the soil water can be further improved, and on the other hand, when the extrusion component 3 finishes extrusion action on the columnar sponge, the columnar sponge is favorable for quickly recovering the original state, and then the soil water can be better adsorbed and stored later. The porous absorbent material 22 may be, but is not limited to, a sponge, and the porous absorbent material 22 may also be a porous material having a certain compression ratio, such as absorbent cotton, nonwoven fabric, or the like.|[0029] Referring to fig. 6, 8 and 9, in some embodiments, the pressing assembly 3 includes a first pressing member 31 slidably disposed in the porous ceramic tube 21, a second pressing member 32 slidably disposed in the porous ceramic tube 21, an elastic member 33 for elastically pressing the second pressing member 32 toward the first pressing member 31, and a push-pull rod 34 for driving the first pressing member 31 to slide toward the second pressing member 32, wherein the first pressing member 31 is disposed adjacent to the closed end of the porous ceramic tube 21, the first pressing member 31 abuts against a first end of the columnar sponge, the second pressing member 32 is disposed adjacent to the open end of the porous ceramic tube 21, the first pressing member 31 abuts against a second end of the columnar sponge, a first sliding hole 323 for the push-pull rod 34 to pass through is disposed on the second pressing member 32, a second sliding hole 221 for the push-pull rod 34 to pass through is disposed on the columnar sponge, the first end of the rod 34 extends into the porous ceramic tube 21 through the open end of the porous ceramic tube 21, and is connected to the first sliding hole 323 and the second sliding hole 221 after sequentially passing through the first sliding hole and the second sliding hole 221, and the second pressing member 31 abuts against a second end of the columnar sponge, and the second end of the rod 34 is connected to the driving device 4. In this embodiment, the driving device 4 pulls the push-pull rod 34 towards the open end of the porous ceramic tube 21, the push-pull rod 34 drives the first pressing member 31 to move towards the second pressing member 32, and as the distance between the first pressing member 31 and the second pressing member 32 gradually decreases, the columnar sponge between the first pressing member 31 and the second pressing member 32 is continuously compressed, and the soil water in the columnar sponge is also continuously extruded in the compression process. In the process of pressing the columnar sponge by the first pressing piece 31 and the second pressing piece 32, the second pressing piece 32 is elastically pressed against the first pressing piece 31 by the elastic piece 33, so that soil water in the columnar sponge is slowly released under the elastic buffering action of the elastic piece 33, the columnar sponge is prevented from being excessively compressed by the first pressing piece 31 and the second pressing piece 32 instantly, the pressure in the porous ceramic tube 21 is instantly increased, the soil water can leak through the micropore structure of the porous ceramic, and the pH value and the ion concentration in the soil water can be changed. Because be equipped with the second slide hole 221 that supplies push-and-pull rod 34 to pass on the column sponge, the column sponge passes through second slide hole 221 cover and locates on the push-and-pull rod 34, in the in-process of first pressure piece 31 and the extrusion of second pressure piece 32 column sponge, not only can effectively avoid the column sponge that axial length is longer to take place distortion, can be favorable to the column sponge later stage to resume original state fast moreover. It should be noted that, a sealing ring is disposed between the push-pull rod 34 and the first sliding hole 323 to enhance the sealing performance of the sliding contact between the push-pull rod 34 and the first sliding hole 323. In addition, locate the column sponge between first pressure piece 31 and the second pressure piece 32 to push up the elasticity of second pressure piece 32 towards first pressure piece 31 through elastic component 33, on the one hand be favorable to high efficiency with the soil water extrusion in the column sponge, on the other hand can push back the column sponge to the position that adsorbs the soil water through the action of pushing up of elastic component 33 fast through the second pressure piece 32.|[0030] Referring to fig. 5, 8 and 9 in combination, in some embodiments, the elastic member 33 is a coil spring accommodated in the porous ceramic tube 21, the open end of the porous ceramic tube 21 is provided with a holding cover 23 for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover 23, the other end of the coil spring is held against the second holding member 32, the holding cover 23 is provided with a third sliding hole 231 through which the push-pull rod 34 passes, and a sealing ring is disposed between the push-pull rod 34 and the third sliding hole 231 to enhance the sealing performance of sliding contact between the push-pull rod 34 and the third sliding hole 231. It should be noted that the holding cover 23 may be, but not limited to, connected to the open end of the porous ceramic tube 21 by a threaded connection, and the elastic member 33 may be, but not limited to, a coil spring.|[0031] Referring to fig. 6, 8 and 9, in some embodiments, the first pressing member 31 includes a first piston 311 slidably disposed in the porous ceramic tube 21 and a first pressing member 312 connected to the first piston 311, the outer peripheral surface of the first piston 311 is in interference contact with the inner sidewall of the porous ceramic tube 21, the first pressing member 312 abuts against the first end of the cylindrical sponge, the first piston 311 is a rubber member or a silicone member having elasticity, the first pressing member 312 is a hard metal sheet or a plastic sheet, and a supporting and reinforcing effect is formed on the first piston 311 by the first pressing member 312, so as to prevent the first pressing member 31 from deforming during the process of pressing the cylindrical spring. Similarly, the second pressing member 32 includes a second pressing member 322 slidably disposed in the porous ceramic tube 21 and connected to the second piston 321, where the outer circumferential surface of the second piston 321 is in interference contact with the inner sidewall of the porous ceramic tube 21, the second pressing member 322 abuts against the second end of the cylindrical sponge, the second piston 321 is a rubber member or a silica gel member having elasticity, and the second pressing member 322 is a hard metal sheet or a plastic sheet, and forms a supporting and reinforcing effect on the second piston 321 by the second pressing member 322, so as to prevent the deformation of the first pressing member 31 in the process of pressing the cylindrical spring.|[0032] Referring to fig. 7, 8 and 9 in combination, in some embodiments, the porous ceramic tube 21 includes a first tube section 211 and a second tube section 212 that are integrally formed, one end of the first tube section 211 away from the second tube section 212 is a closed end, one end of the second tube section 212 away from the first tube section 211 is an open end, a microporous structure capable of adsorbing and transmitting soil water is provided on a tube wall of the first tube section 211, the first piston 311 and the columnar sponge are located in the first tube section 211, and the soil water can be adsorbed and transmitted to the columnar sponge in the first tube section 211 by capillary action of the microporous structure. Meanwhile, the pipe wall of the second pipe section 212 is of a dense structure which is airtight and watertight, and the second piston 321 and the elastic piece 33 are located in the second pipe section 212, so that the elastic piece 33 in the second pipe section 212 cannot pollute soil water, and meanwhile, the soil water cannot flow into the second pipe section 212 to erode the elastic piece 33. It should be noted that, when the first pressing member 31 drives the columnar sponge into the second pipe section 212, the elastic member 33 is in a compressed state, and the elastic member 33 can elastically press the second pressing member 32 against the first pressing member 31, so that the second pressing member 32 cooperates with the first pressing member 31 to compress the columnar sponge into the sealed second pipe cavity, and the soil water extruded from the columnar sponge flows out through the water outlet 213 on the pipe wall of the second pipe section 212. In addition, when the second pressing member 32 compresses the columnar sponge in the sealed second lumen in cooperation with the first pressing member 31, the pressure in the second tube section 212 can be increased, so that the soil water in the second tube section 212 is pressed out, and the collection efficiency of the soil water can be accelerated.|[0033] Referring to fig. 1, 2 and 3, in some embodiments, in order to collect soil water more quickly and efficiently, a plurality of soil water adsorbing assemblies 2 are arranged, and a plurality of soil water adsorbing assemblies 2 are arranged side by side and at intervals, and each soil water adsorbing assembly 2 is provided with a squeezing assembly 3 in a matching manner, and each squeezing assembly 3 is connected with a driving device 4.|[0034] Referring to fig. 1, 2 and 3, in some embodiments, the driving device 4 includes a sliding rod 41 with two ends slidably disposed on the fixed support 1, a driving rod 42 for driving the sliding rod 41 to move along the axial direction of the push-pull rod 34, and an air cylinder 43 for driving the driving rod 42 to move along the axial direction, the fixed support 1 is provided with a sliding groove 11, and two ends of the sliding rod 41 are slidably inserted into the sliding groove 11. The axial direction of the sliding rod 41 is perpendicular to the axial direction of the sliding rod 34, the second end of the sliding rod 34 is connected with the sliding rod 41, the axial direction of the driving rod 42 is parallel to the axial direction of the sliding rod 34, the first end of the driving rod 42 is connected with the central position of the sliding rod 34, and the second end of the driving rod 42 is connected with a piston rod 431 of the air cylinder 43. In this embodiment, the push-pull rod 34 is driven to axially move by the telescopic movement of the piston rod 431 of the air cylinder 43, so that the driving rod 42 can be driven to axially move along the driving rod 42 by the push-pull rod 34, the sliding rod 41 further drives the push-pull rod 34 to axially move, and the push-pull rod 34 drives the first pressing member 31 to reciprocate along the axial direction of the porous ceramic tube 21, so that the columnar sponge can be pressed by the first pressing member 31 and the second pressing member 32. It should be noted that, the fixed bracket 1 is provided with a sliding slot, two ends of the sliding rod 41 are respectively disposed in the corresponding sliding slots, the fixed bracket 1 is further provided with a fourth sliding hole, and the driving shaft is slidably inserted into the fourth sliding hole.|[0035] Referring to fig. 1,2 and 3 in combination, in some embodiments, in order to enhance the stability of the movement of the push-pull rod 34 driven by the driving device 4 and to maintain the high precision operation of the push-pull rod 34, the number of the air cylinders 43 is two, the piston rods 431 of the two air cylinders 43 are symmetrically distributed with the central axis of the driving rod 42 as a symmetrical axis, the driving device 4 further comprises a connecting rod 49 axially perpendicular to the axial direction of the push-pull rod 34 and two pulley blocks 44 symmetrically arranged at two sides of the driving rod 42, each pulley block 44 is wound with a pull rope 45, the axial direction of the vertical section 451 of each pull rope 45 is parallel to the axial direction of the push-pull rod 34, one pull rope 45 connects the first end of the sliding rod 41 with the first end of the connecting rod 49, the other pull rope 45 connects the second end of the sliding rod 41 with the second end of the connecting rod 49, and the two ends of the connecting rod 49 are respectively connected with the corresponding piston rods 431, and the second end of the driving rod 42 is connected with the central position of the connecting rod 49. It should be noted that, each pulley block 44 includes at least one fixed pulley 441 and at least one movable pulley 442, the fixed pulley 441 is rotatably disposed on the fixed bracket 1 through the first pulley bracket 46, the first pulley bracket 46 is fixedly connected with the fixed bracket 1, the movable pulley 442 is rotatably disposed on the fixed bracket 1 through the second pulley bracket 47, and the second pulley bracket 47 is fixedly connected with the fixed bracket 1. Specifically, the fixed support 1 is provided with a second pulley support 47, the second pulley support 47 is provided with a sliding groove or a bar-shaped sliding hole 48 capable of guiding the movable pulley 442 to slide along the axial direction of the driving rod 42, and two sections of sliding shafts 7 respectively inserted into the sliding groove or the bar-shaped sliding hole 48, and the movable pulley 442 is slidably arranged on the guiding support 48 through a sliding matching structure of the sliding shafts 7 and the sliding groove or the bar-shaped sliding hole 48.|[0036] It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled. Of course, the filter layer may also include at least one layer of sediment filter screen, and the filter layer may also be in other structural forms capable of blocking sediment outside the filter layer. It should be noted that the filter layer includes at least one layer of non-woven fabric or silt filter screen, which means that the filter layer wrapped on the outer side of the porous ceramic tube 21 may be a layer structure or a multi-layer structure, and is determined according to the filtering effects of different filtering materials and structures.|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention. Family Number|(117274553)|117274553|Abstract|(CN121253236 A)|The invention provides a buried soil water collection system , and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance , a porous ceramic tube is buried in soil , a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube , and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action , so that the soil water is absorbed by the porous ceramic tube ; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube , and the porous water absorption material can continuously adsorb and store the soil water . When the water storage amount in the porous water absorption material is sufficient , the extrusion assembly is driven by the driving device to extrude the porous water absorption material , so that the soil water stored in the porous water absorption material is extruded out , and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe , so that the soil water is centrally stored in the water storage container . Therefore , the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in - situ structure and the moisture dynamic state of the soil are not damaged . |CPC codes|(CN121253236 A)|G01N - 001/20/35 |G01N - 001/20 |G01N - 2001/2021 |G01N - 2001/205 |IPC codes|(CN121253236 A)|G01N - 001/20 | Measurement G01N-001/20|G01N-001/20/35|G01N-2001/2021|G01N-2001/205 G01N-001/20|G01N-001/20/35|G01N-2001/2021|G01N-2001/205 G01N-001/20 G01N-001/20 PENDING (CN121253236)|PENDING ALIVE (CN121253236)|ALIVE (CN121253236)|LEGAL DETAILS FOR CN121253236|Actual or expected expiration date=2045-10-29|Legal state=ALIVE|Status=PENDING|Event publication date=2025-10-29|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202511559558|Application date=2025-10-29|Standardized application number=2025CN-1559558|Event publication date=2026-01-02|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN121253236|Publication stage code=A|Publication date=2026-01-02|Standardized publication number=CN121253236|Event publication date=2026-01-02|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2026-01-20|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN121253236)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfJWdolE5dLe1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080386811&ekey=1806&xpn=CN121253236&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=gPZaP4yiAL%252BirZpns%252Bzw6pNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN121253236)|CN (CN121253236)|NAME=LANZHOU UNIVERSITY , COUNTRY=CN (CN121253236)|NAME=HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=41028 (CN121253236)|CN (CN121253236)|NAME=ZHANG JIETANG, COUNTRY=CN |NAME=LI XINGYUAN|NAME=GOU XIAOHUA 0 1 Titre: (CN121253236)|Buried soil water collecting system Résumé: (CN121253236)|The invention provides a buried soil water collection system, and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance, a porous ceramic tube is buried in soil, a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube, and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action, so that the soil water is absorbed by the porous ceramic tube; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube, and the porous water absorption material can continuously adsorb and store the soil water. When the water storage amount in the porous water absorption material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorption material, so that the soil water stored in the porous water absorption material is extruded out, and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe, so that the soil water is centrally stored in the water storage container. Therefore, the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. 115 Abstract gpt-4o-mini no The article focuses on a soil water collection system and does not address accelerated weathering or CO₂ capture.
118 CN202311184117 CN202311184117 CN117163943|CN117163943 107609891 CN117163943 B 2025-09-12 [CN117163943B]|CN117163943 A 2023-12-05 [CN117163943] 2023-09-14 2023-09-14 2025-09-12|2023-12-05 (CN117163943B)|2025-09-12 (CN117163943)|2043-09-14 (CN117163943)|Preparation method of carbon aerogel material used as silicon-carbon negative electrode (CN117163943)|The invention discloses a preparation method of a carbon aerogel material used as a silicon-carbon negative electrode, which comprises the following steps: by taking phenolic resin as a main raw material, carrying out sol-gel treatment, crushing, drying, grading, carbon activation, impurity removal, grinding and the like, adjusting the pore structure distribution of carbon aerogel, and controlling the indexes such as impurity content, ash content, water content, particle size distribution and the like, so as to prepare the carbon aerogel material used as the silicon-carbon negative electrode. The use requirements of the silicon-carbon negative electrode field on the carbon aerogel are met. The prepared carbon aerogel material has a specific surface area of 1000-3000 m < 2 >/g, a pore volume of 0.3-2 cm < 3 >/g, an average pore size of 0.5-10 nm and a micropore proportion of 30-100%, and can be used as a porous carbon matrix material of a silicon-carbon negative electrode. Phenolic resin, formaldehyde, potassium hydroxide and the like are used as main raw materials, so that the cost is low; the material is graded and then subjected to carbon activation, the controllability and consistency of the material in the carbon activation process are guaranteed, meanwhile, the impurity removal technology is simple, the whole technology is efficient, and large-scale production of the carbon aerogel material is facilitated. SINOSTEEL MAANSHAN GENERAL INSTITUTE OF MINING RESEARCH|SINOSTEEL MIMR NEW MATERIAL TECHNOLOGY (CN117163943)|SINOSTEEL MAANSHAN GENERAL INSTITUTE OF MINING RESEARCH CO., LTD ([CN])|SINOSTEEL MIMR NEW MATERIAL TECHNOLOGY CO., LTD|(CN117163943)|SINOSTEEL MAANSHAN GENERAL INSTITUTE OF MINING RESEARCH CO., LTD ([CN])|SINOSTEEL MIMR NEW MATERIAL TECHNOLOGY CO., LTD WANG JUN|JIN LIANG|PAN ZHE|LIU YAHUI (CN117163943)|WANG JUN|JIN LIANG|PAN ZHE|LIU YAHUI|(CN117163943)|WANG JUN|JIN LIANG|PAN ZHE|LIU YAHUI (CN117163943)|CHANG QIANFA;MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. MA'ANSHAN CITY JINQIAO PATENT AGENT LTD.|Reg. Nb: 34111|XI ZHIPENG;MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. MA'ANSHAN CITY JINQIAO PATENT AGENT LTD.|Reg. Nb: 34111 (CN117163943)|Compared with the prior art, the preparation method of the carbon aerogel material used as the silicon-carbon negative electrode has the following advantages:|The inorganic silicon material has the advantages of high earth element abundance, good safety, easy industrialization and the like. As a lithium battery anode material, the huge theoretical specific capacity (4200 mAh/g) of the lithium battery anode material has the unique advantage of preparing a high-performance anode material.|The invention aims to solve the problems of complex process, high production cost, low porosity, unreasonable pore structure distribution, poor product consistency, low purity and difficult mass production in the prior art, and provides a preparation method of a carbon aerogel material used as a silicon-carbon negative electrode, wherein the preparation method has the advantages of wide raw material source, simple production process, high product purity, reasonable pore size and reasonable distribution.|Currently, in various lithium ion battery anode materials, graphite anode occupies the main market, but the theoretical capacity of graphite is only 372mAh/g, so that the requirement of higher energy density is difficult to meet, and a novel anode material needs to be developed.|In the method, commercial nano silicon is used as a raw material, the cost is high, in addition, only some holes are formed on the surface of the carbon material, nano silicon particles which can be embedded are limited, and the nano silicon particles are difficult to uniformly enter the pores of the carbon material, so that the excellent performance of the silicon-carbon material cannot be fully exerted.| (CN117163943)|1. The preparation method of the carbon aerogel material used as the silicon-carbon negative electrode is characterized by comprising the following steps: 1) Sol-gel, namely mixing and dissolving a set amount of phenolic resin, formaldehyde aqueous solution, potassium hydroxide and a pore-forming agent, and preserving heat for a period of time at a certain temperature T1 to obtain a gel material, wherein the molar ratio of the phenolic resin to formaldehyde is 1:1-3.5, the molar ratio of the phenolic resin to the potassium hydroxide is 10-200:1, the pore-forming agent is cetyl trimethyl ammonium bromide, the adding proportion of the pore-forming agent is 1-10% of the mass of the phenolic resin, the temperature T1 is 60-80 ℃, and the preserving heat time is 5-15 h; 2) Crushing, namely crushing the gel material to obtain fine particle gel material with certain particle size distribution, and controlling the D50 of the fine particle gel material to be in a range of 100-600 mu m; 3) Drying, namely drying the fine-particle gel material in drying equipment at a certain temperature T2 for a period of time to obtain a dried material, wherein the temperature T2 is 80-150 ℃, the drying time is 10-20 h, and the water content of the dried material is less than or equal to 1%; 4) Classifying, namely classifying the dried material by classifying equipment to obtain classified material, wherein the granularity D50 of the classified material is controlled to be 300-500 mu m, and the (D90-D10)/D50 is less than or equal to 1.5; 5) Carbonizing, namely carbonizing the grading material under the protection of certain carbonization temperature, time and inert gas to obtain carbonized material, wherein the carbonization temperature is controlled in the range of 600-1000 ℃; 6) Activating, namely activating the carbonized material at a certain activation temperature, time and an activating agent atmosphere to obtain an activated material, wherein the activating agent is one or a mixture of water vapor and carbon dioxide, and the activation temperature is controlled to be 700-1000 ℃; 7) Removing impurities, namely removing iron impurities from the activated material through magnetic separation equipment to obtain a pure material; 8) Grinding, namely carrying out further grinding treatment on the pure material to obtain a carbon aerogel material finished product with the specific surface area of 1000-3000 m 2/g, the pore volume of 0.3-2 cm 3/g, the average pore diameter of 0.5-10 nm and the micropore ratio of less than 2 nanometers of 30% -100%. | (CN117163943)|The invention discloses a preparation method of a carbon aerogel material used as a silicon-carbon anode, which comprises the following steps:|The invention discloses a preparation method of a carbon aerogel material used as a silicon-carbon negative electrode, which adopts phenolic resin as a main raw material, and adopts the steps of sol-gel, crushing, drying, grading, carbon activation, impurity removal, grinding and the like to adjust the pore structure distribution of the carbon aerogel, control the indexes of impurity content, ash content, water content, particle size distribution and the like, so as to meet the use requirement of the silicon-carbon negative electrode field on the carbon aerogel.| (CN117163943)|CARBON AEROGEL(100,32)|SILICON CARBON NEGATIVE ELECTRODE(100,15)|NEGATIVE ELECTRODE(100,13)|NANO SILICON PARTICLE(81,2)|TECHNOLOGICAL PARAMETER(61,5)|MICROPORE RATIO(53,16)|NANO SILICON(52,1)|GRAPHITE ANODE(51,1)|REMOVING IMPURITY(48,5)|IMPURITY CONTENT(48,1)|ASH CONTENT(46,1)|PHENOLIC RESIN(44,16)|PORE VOLUME(43,18)|CARBONIZATION TEMPERATURE(43,5)|MEDIAN PORE DIAMETER(41,15)|INDUSTRIALIZATION(41,1)|ACTIVATING AGENT ATMOSPHERE(40,2)|IRON IMPURITY REMOVAL(39,3)|GRINDING TREATMENT(39,2)|PHENOLIC RESIN MOLAR RATIO(38,6)|GRADING(37,5)|EQUIPMENT CLASSIFICATION(37,3)|CENTRIFUGAL MILL(37,1)|CRUSHING(34,6)|MOLAR RATIO(34,6)|PRODUCT CONSISTENCY(34,1)|VIBRATION MILL(34,1)|GRINDING(31,5)|FORMALDEHYDE AQUEOUS SOLUTION(31,3)|GRANULARITY(31,2)|FINE PARTICLE(30,5)|FORMALDEHYDE(30,5)|PRODUCT PURITY(30,1)|UNREASONABLE PORE STRUCTURE DISTRIBUTION(30,1)|ACTIVATION TEMPERATURE(29,8)|POTASSIUM HYDROXIDE(28,8)|CARBON ACTIVATION(27,4)|HEAT PRESERVATION(27,3)|POROUS CARBON MATRIX(27,2)|DRYING EQUIPMENT(26,3)|CONTROLLABILITY(26,1)|EARTH ELEMENT ABUNDANCE(26,1)|PORE STRUCTURE(25,5)|LITHIUM BATTERY ANODE MATERIAL(25,2)|ACTIVATION(24,4)|ANODE MATERIAL(24,4)|PORE SIZE(24,1)|POROSITY(21,3)|SILICON CARBON ANODE(21,3)|HUGE THEORETICAL SPECIFIC CAPACITY(21,1)|PRODUCTION COST(21,1)|AQUEOUS SOLUTION(20,3)|DRIED MATERIAL(19,9)|PURITY(19,2)|CETYL TRIMETHYL AMMONIUM BROMIDE(17,3)|INORGANIC SILICON MATERIAL(17,1)|CARBONIZED MATERIAL(16,4)|MAGNETIC SEPARATION EQUIPMENT(15,6)|WATER CONTENT(14,3)|CARBON ACTIVATION(14,1)|DIFFICULT MASS PRODUCTION(14,1)|IMPURITY REMOVAL(14,1)|MAGNETIC SEPARATION(13,7)|CARBON MATERIAL(13,5)|HELIUM(13,2)|CARBON DIOXIDE(12,3)|PRESERVING HEAT TIME(12,1)|GEL MATERIAL(11,3)|MATERIAL ACTIVATION(11,3)|ARGON(11,2)|INERT GAS(11,2)|NEGATIVE ELECTRODE FIELD(11,2)|INERT ATMOSPHERE(10,2)|SILICON CARBON(10,2)|ENDURANCE MILAGE(10,1)|CLASSIFIED MATERIAL(9,6)|LITHIUM ION BATTERY(9,6)|RAW MATERIAL(9,6)|CRUSHED GEL(9,2)|DRYING TIME(9,2)|ENERGY DENSITY(9,2)|MATERIAL IRON CONTENT(9,2)|WATER VAPOR(9,2)|CARBONIZATION TIME(8,2)|ENERGY AUTOMOBILE(7,2)|PREPARING CARBON AEROGEL MATERIAL(7,2)|SILICON NEGATIVE ELECTRODE(7,2)|TECHNICAL PARAMETER(7,2)|MAH G(7,1)|MARKET ADAPTABILITY(7,1)|PARTICLE SIZE DISTRIBUTION(6,8)|MATERIAL FINISHED PRODUCT(6,6)|CARBON AEROGEL POWDER(6,3)|SILICON CARBON NEGATIVE ELECTRODE FIELD(6,2)|ACTIVATION UNIFORMITY(6,1)|HIGH SPEED CENTRIFUGAL MILL(6,1)|ORGANIC AEROGEL POWDER(6,1)|RESORCINOL FORMALDEHYDE SOLUTION(6,1)|ACTIVATION TIME(5,3)|CAPACITY(5,3)|CARBON AEROGEL MICROPORE RATIO(5,1)|CATALYST PROPORTION(5,1)|GRINDING FREQUENCY(5,1)|GRINDING MACHINE CENTRIFUGATION(5,1)|ICP EQUIPMENT(5,1)|PORE DIAMETER ANALYZER(5,1)|SILICON ANODE(5,1)|TECHNICAL ROUTE(5,1)|WIDE RAW MATERIAL SOURCE(5,1)|RAW MATERIAL SOURCE(4,2)|ACIDIC WASH(3,1)|AVERAGE GRAIN DIAMETER(3,1)||(CN117163943)|CARBON AEROGEL(100,27)|SILICON CARBON NEGATIVE ELECTRODE(100,13)|NEGATIVE ELECTRODE(100,8)|NANO SILICON PARTICLE(94,2)|SILICON CARBON ANODE(82,8)|TECHNOLOGICAL PARAMETER(71,5)|MICROPORE RATIO(62,16)|GRAPHITE ANODE(59,1)|REMOVING IMPURITY(56,5)|IMPURITY CONTENT(56,1)|ACTIVATOR ATMOSPHERE(53,2)|ASH CONTENT(53,1)|MEDIAN PORE DIAMETER(51,10)|GRADING(51,8)|IRON IMPURITY(51,2)|PORE VOLUME(50,18)|CARBONIZATION TEMPERATURE(50,5)|INDUSTRIALIZATION(47,1)|CARBON ACTIVATION(42,5)|EQUIPMENT CLASSIFICATION(42,3)|NANO SILICON(42,3)|PHENOLIC RESIN(41,16)|CRUSHING(39,6)|MICROPORE(39,4)|PRODUCT CONSISTENCY(39,1)|GRANULARITY(36,2)|GRINDING(35,6)|FINE PARTICLE(35,5)|FORMALDEHYDE AQUEOUS SOLUTION(35,3)|PRODUCT PURITY(35,1)|UNREASONABLE PORE STRUCTURE DISTRIBUTION(35,1)|ACTIVATOR(34,2)|ACTIVATION TEMPERATURE(33,8)|MATERIAL TOFURTHER(32,1)|GRAM(31,20)|HEAT PRESERVATION(31,3)|CONTROLLABILITY(31,1)|EARTH ELEMENT ABUNDANCE(31,1)|DRYING EQUIPMENT(30,3)|PORE STRUCTURE(29,5)|LITHIUM BATTERY ANODE MATERIAL(29,2)|POTASSIUM HYDROXIDE(28,8)|ANODE MATERIAL(28,4)|PORE SIZE(28,1)|PHENOLIC RESIN MOLAR RATIO(27,6)|GRINDING MACHINE CENTRIFUGATION(25,2)|HUGE THEORETICAL SPECIFIC CAPACITY(25,1)|PRODUCTION COST(25,1)|POROSITY(24,3)|AQUEOUS SOLUTION(23,3)|PURITY(23,2)|STEAM(23,2)|VIBRATION GRINDING MACHINE(23,2)|MAGNETIC SEPARATION EQUIPMENT(22,7)|MATERIALSRAW MATERIAL(22,1)|INORGANIC SILICON MATERIAL(20,1)|DRIED MATERIAL(19,9)|MATERIAL ACTIVATION(19,5)|CARBONIZED MATERIAL(19,4)|IMPURITY REMOVAL(17,1)|CARBON ACTIVATION(16,1)|DIFFICULT MASS PRODUCTION(16,1)|MAGNETIC SEPARATION(15,7)|CARBON MATERIAL(15,5)|HELIUM(15,2)|CARBON DIOXIDE(14,3)|POROUS CARBON MATRIX MATERIAL(14,1)|CETYL TRIMETHYL AMMONIUM BROMIDE(13,3)|ARGON(13,2)|INERT GAS(13,2)|NEGATIVE ELECTRODE FIELD(13,2)|INERT ATMOSPHERE(12,2)|SILICON CARBON(12,2)|GEL MATERIAL(11,5)|WATER CONTENT(11,4)|ENERGY DENSITY(11,2)|ENDURANCE MILAGE(11,1)|CLASSIFIED MATERIAL(10,6)|LITHIUM ION BATTERY(10,6)|MATERIAL IRON CONTENT(10,2)|AVERAGE APERTURE(9,5)|CARBONIZATION TIME(9,2)|CRUSHED GEL(9,2)|SILICON ANODE(9,2)|RAW MATERIAL(8,5)|ENERGY AUTOMOBILE(8,2)|PREPARING CARBON AEROGEL MATERIAL(8,2)|TECHNICAL PARAMETER(8,2)|MAH G(8,1)|MARKET ADAPTABILITY(8,1)|PARTICLE SIZE DISTRIBUTION(7,6)|CARBON AEROGEL POWDER(7,3)|HEAT PRESERVATION TIME(7,2)|SILICON CARBON NEGATIVE ELECTRODE FIELD(7,2)|ACTIVATION UNIFORMITY(7,1)|ADDITION RATIO(7,1)|IRON IMPURITY REMOVAL(7,1)|ORGANIC AEROGEL POWDER(7,1)|RESORCINOL FORMALDEHYDE SOLUTION(7,1)|ACTIVATION TIME(6,3)|CAPACITY(6,3)|DRYING TIME(6,2)|SILICON CARBON CATHODE(6,2)|CARBON AEROGEL MICROPORE RATIO(5,1)|CATALYST PROPORTION(5,1)|GRINDING FREQUENCY(5,1)|ICP EQUIPMENT(5,1)|PORE DIAMETER ANALYZER(5,1)|TECHNICAL ROUTE(5,1)|WIDE RAW MATERIAL SOURCE(5,1)| (CN117163943)|1. The preparation method of the carbon aerogel material used as the silicon-carbon negative electrode is characterized by comprising the following steps:| 1) Sol-gel, namely mixing and dissolving a set amount of phenolic resin, formaldehyde aqueous solution, potassium hydroxide and a pore-forming agent, and preserving heat for a period of time at a certain temperature T1 to obtain a gel material, wherein the molar ratio of the phenolic resin to formaldehyde is 1:1-3.5, the molar ratio of the phenolic resin to the potassium hydroxide is 10-200:1, the pore-forming agent is cetyl trimethyl ammonium bromide, the adding proportion of the pore-forming agent is 1-10% of the mass of the phenolic resin, the temperature T1 is 60-80 ℃, and the preserving heat time is 5-15 h; | 2) Crushing, namely crushing the gel material to obtain fine particle gel material with certain particle size distribution, and controlling the D50 of the fine particle gel material to be in a range of 100-600 mu m; | 3) Drying, namely drying the fine-particle gel material in drying equipment at a certain temperature T2 for a period of time to obtain a dried material, wherein the temperature T2 is 80-150 ℃, the drying time is 10-20 h, and the water content of the dried material is less than or equal to 1%; | 4) Classifying, namely classifying the dried material by classifying equipment to obtain classified material, wherein the granularity D50 of the classified material is controlled to be 300-500 mu m, and the (D90-D10)/D50 is less than or equal to 1.5; | 5) Carbonizing, namely carbonizing the grading material under the protection of certain carbonization temperature, time and inert gas to obtain carbonized material, wherein the carbonization temperature is controlled in the range of 600-1000 ℃; | 6) Activating, namely activating the carbonized material at a certain activation temperature, time and an activating agent atmosphere to obtain an activated material, wherein the activating agent is one or a mixture of water vapor and carbon dioxide, and the activation temperature is controlled to be 700-1000 ℃; | 7) Removing impurities, namely removing iron impurities from the activated material through magnetic separation equipment to obtain a pure material; | 8) Grinding, namely carrying out further grinding treatment on the pure material to obtain a carbon aerogel material finished product with the specific surface area of 1000-3000 m 2/g, the pore volume of 0.3-2 cm 3/g, the average pore diameter of 0.5-10 nm and the micropore ratio of less than 2 nanometers of 30% -100%. |2. The method for preparing the carbon aerogel material used as the silicon-carbon negative electrode according to claim 1, wherein the carbonization time in the step 5) is 2-4 hours, the inert atmosphere is nitrogen, helium or argon, and the activation time in the step 6) is 6-15 hours.|3. The method of claim 2, wherein in step 7), the magnetic field strength of the magnetic separation device is controlled so that the iron content of the pure material is less than or equal to 100ppm.|4. The method for preparing a carbon aerogel material for a silicon-carbon negative electrode according to claim 3, wherein in the step 8), equipment used in the grinding operation is a vibration mill or a high-speed centrifugal mill, the frequency is 20-45 Hz, and the particle size distribution D50 of the finished product of the carbon aerogel material is 2-15 μm.|5. The method for preparing the carbon aerogel material used as the silicon-carbon negative electrode according to claim 4, wherein the technological parameters of each step are controlled to obtain a carbon aerogel material finished product with the specific surface area of 1150-640 m 2/g, the pore volume of 0.45-0.60 cm 3/g, the average pore diameter of 1.5-2.5 nm and the micropore ratio of less than 2 nanometers of 80% -100%.|6. The method for preparing the carbon aerogel material used as the silicon-carbon negative electrode according to claim 4, wherein the specific surface area is 1750-1950 mm 2/g, the pore volume is 0.75-0.90 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio smaller than 2 nm is 80% -100% by controlling the technological parameters of each step.|7. The method for preparing the carbon aerogel material used as the silicon-carbon negative electrode according to claim 4, wherein the specific surface area is 2150-2350 m 2/g, the pore volume is 0.95-1.10 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio smaller than 2 nm is 80% -100% by controlling the technological parameters of each step. (CN117163943)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of preparation of lithium ion battery materials, and particularly relates to a preparation method of a porous carbon matrix material of a silicon-carbon negative electrode.|BACKGROUND ART|[0002] Lithium ion batteries have been rapidly developed since the 70 s of the 20 th century, have the characteristics of high energy density, long cycle life and the like, and have been widely applied to the fields of portable electronic devices, vehicles, energy storage power stations and the like, particularly in the field of new energy automobiles, and have been in great demand in recent years. Along with the increasing demands of people on higher endurance mileage, shorter charging time and the like of new energy automobiles, higher demands are also put forward on the energy density of lithium batteries. Currently, in various lithium ion battery anode materials, graphite anode occupies the main market, but the theoretical capacity of graphite is only 372mAh/g, so that the requirement of higher energy density is difficult to meet, and a novel anode material needs to be developed.|[0003] The inorganic silicon material has the advantages of high earth element abundance, good safety, easy industrialization and the like. As a lithium battery anode material, the huge theoretical specific capacity (4200 mAh/g) of the lithium battery anode material has the unique advantage of preparing a high-performance anode material. However, when silicon is charged and discharged, the silicon material is pulverized in the circulation process due to the huge volume change effect (> 300%), so that various performances of the battery are deteriorated. In addition, silicon is a common semiconductor material, and has poor conductive performance, so that the cycle performance of the silicon anode material in a lithium ion battery is affected.|[0004] In recent years, in order to utilize the high specific capacity of silicon and suppress the volume expansion effect thereof, researchers have conducted a great deal of research, and among them, a preferred technical route is to prepare a silicon/carbon composite material while utilizing the high specific capacity of silicon and good mechanical properties and electrical conductivity of the carbon material.|[0005] Chinese patent CN110098380A discloses a preparation method of a silicon-based negative electrode material of a lithium ion battery, which comprises the steps of firstly etching the surface of a carbon material by adopting a physical or chemical method, forming a plurality of nano-to micron-sized holes on the surface of the carbon material, then carrying out mixed ball milling on the prepared carbon material with the holes and nano-silicon with a certain proportion, embedding the nano-silicon into the holes of the carbon material, and finally carrying out carbon coating treatment on the material after mixed ball milling to obtain the silicon-based negative electrode material of the lithium ion battery. In the method, commercial nano silicon is used as a raw material, the cost is high, in addition, only some holes are formed on the surface of the carbon material, nano silicon particles which can be embedded are limited, and the nano silicon particles are difficult to uniformly enter the pores of the carbon material, so that the excellent performance of the silicon-carbon material cannot be fully exerted. Obviously, the carbon material with high porosity and reasonable pore structure distribution is the basis for the performance of the silicon-carbon anode material. The carbon aerogel has the excellent properties of high porosity, adjustable pore structure and the like, and has great application potential in the field of silicon-carbon cathodes.|[0006] In terms of a preparation method of carbon aerogel, chinese patent CN1895770a discloses a "preparation method of carbon aerogel powder", in which resorcinol-formaldehyde solution containing a certain concentration and a catalyst proportion is uniformly dispersed in an oil phase under the action of ultrasonic wave and at low temperature, and gel polymerization reaction is performed under heating and ultrasonic wave, and organic aerogel powder is obtained through separation and cleaning, and then carbon aerogel powder is obtained through carbon activation. The method uses resorcinol as the raw material, has high cost, can generate a large amount of organic oil to be treated in the production process, has complex process and is not beneficial to large-scale production.|[0007] In conclusion, whether the carbon aerogel material with high purity and reasonable pore structure distribution can be prepared by using a simpler process is a key for improving the performance of the silicon-carbon negative electrode material.|DISCLOSURE|Disclosure of Invention|[0008] The invention aims to solve the problems of complex process, high production cost, low porosity, unreasonable pore structure distribution, poor product consistency, low purity and difficult mass production in the prior art, and provides a preparation method of a carbon aerogel material used as a silicon-carbon negative electrode, wherein the preparation method has the advantages of wide raw material source, simple production process, high product purity, reasonable pore size and reasonable distribution.|[0009] In order to achieve the above purpose, the preparation method of the carbon aerogel material used as the silicon-carbon negative electrode adopts phenolic resin as a main raw material, and the pore structure distribution of the carbon aerogel is adjusted through the steps of sol-gel, crushing, drying, grading, carbon activation, impurity removal, grinding and the like, so that the use requirement of the silicon-carbon negative electrode field on the carbon aerogel is met. The method specifically comprises the following process and steps:|[0010] 1) Sol-gel, namely mixing and dissolving a set amount of phenolic resin, formaldehyde aqueous solution, potassium hydroxide and pore-forming agent, and preserving heat for a period of time at a certain temperature T1 to obtain gel material; |[0011] In the step, the molar ratio of the phenolic resin to formaldehyde is generally 1:1-3.5, preferably 1:1.5-2.5, the molar ratio of the phenolic resin to potassium hydroxide is generally 10-200:1, preferably 40-80:1, the pore-forming agent is preferably cetyl trimethyl ammonium bromide, and the addition ratio of the pore-forming agent is generally 1-10% of the mass of the phenolic resin, preferably 1.5-4.0%; |[0012] In the step, the temperature T1 is 60-80 ℃, and the heat preservation time is 5-15 h. |[0013] 2) Crushing, namely crushing the gel material to obtain fine particle gel material with certain particle size distribution, wherein the D50 of the fine particle gel material is controlled within the range of 100-600 mu m, and preferably 300-600 mu m.|[0014] 3) Drying, namely placing the fine-particle gel material into drying equipment for drying, and obtaining a dried material after a period of time at a certain temperature T2;|[0015] in the step, the temperature T2 is preferably 80-150 ℃, preferably 85-95 ℃, the drying time is 10-20 h, and the moisture content of the dried material is controlled to be less than or equal to 1%. |[0016] 4) Classifying, namely classifying the dried material by classifying equipment to obtain classified material, wherein the granularity D50 of the classified material is controlled to be 300-500 mu m, and the (D90-D10)/D50 is less than or equal to 1.5;|[0017] In this step, D50 is preferably in the range of 400 to 500 μm, and (D90-D10)/D50 is preferably not more than 1.2. |[0018] 5) Carbonizing, namely carbonizing the grading material under the protection of certain carbonization temperature, time and inert gas to obtain carbonized material, wherein the carbonization temperature is controlled in the range of 600-1000 ℃;|[0019] The carbonization time is 2-4h, the carbonization temperature is controlled within the range of 650-800 ℃, the inert atmosphere is one or a mixture of two or more of nitrogen, helium or argon, and the cost of the nitrogen is the lowest. |[0020] 6) Activating, namely activating the carbonized material at a certain activation temperature, time and an activating agent atmosphere to obtain an activated material, wherein the activating agent is one or a mixture of water vapor and carbon dioxide, and the activation temperature is controlled to be 700-1000 ℃;|[0021] In the step, the activation time is controlled to be 6-15 h, preferably 7-10 h, and the activation temperature is controlled to be 750-850 ℃. |[0022] 7) Removing impurities, namely removing iron impurities from the activated material through magnetic separation equipment to obtain a pure material;|[0023] in the step, the selected magnetic separation equipment is preferably dry magnetic separation equipment, such as a Chinese patent ZL201610978391.3 'a dry iron removal device for hollow glass beads', and the magnetic field intensity of the magnetic separation equipment is controlled to ensure that the iron content of the pure material is less than or equal to 100ppm. |[0024] 8) Grinding, namely carrying out further grinding treatment on the pure material to obtain a carbon aerogel material finished product with the specific surface area of 1000-3000 m 2/g, the pore volume of 0.3-2 cm 3/g, the average pore diameter of 0.5-10 nm and the micropore ratio of less than 2 nanometers of 30% -100%.|[0025] In the step 8), equipment adopted in the grinding operation is a vibration grinding machine or a high-speed centrifugal grinding machine, the frequency is 20-45 Hz, 30-40 Hz is preferred, and the particle size distribution D50 of the carbon aerogel material finished product is 2-15 mu m.|[0026] Experimental study shows that the carbon aerogel material finished product with the following product performances can be obtained by controlling the technological parameters of each step:|[0027] ① The specific surface area is 1000-3000 m 2/g, the pore volume is 0.3-2 cm 3/g, the average pore diameter is 0.5-10 nm, and the micropore ratio is 30% -100%; |[0028] ② The specific surface area is 1100-2400 m 2/g, the pore volume is 0.4-1.5 cm 3/g, the average pore diameter is 1.5-3 nm, and the micropore ratio is 60% -100%; |[0029] ③ The specific surface area is 1150-640 m 2/g, the pore volume is 0.45-0.60 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0030] ④ The specific surface area is 1350-1550 m 2/g, the pore volume is 0.55-0.70 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0031] ⑤ The specific surface area is 1550-1750 m 2/g, the pore volume is 0.65-0.80 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0032] ⑥ The specific surface area is 1750-1950 m 2/g, the pore volume is 0.75-0.90 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0033] ⑦ The specific surface area is 1950-2150 m 2/g, the pore volume is 0.85-1.00 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0034] ⑧ The specific surface area is 2150-2350 m 2/g, the pore volume is 0.95-1.10 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%. |[0035] Micropores herein refer to pores of less than 2 nanometers.|[0036] Compared with the prior art, the preparation method of the carbon aerogel material used as the silicon-carbon negative electrode has the following advantages:|[0037] (1) The invention uses phenolic resin, formaldehyde, potassium hydroxide and the like as main raw materials, has wide raw material sources, low cost, relatively simple preparation process and high production efficiency, and is suitable for reference in large-scale industrial production. |[0038] (2) Compared with the traditional process for preparing the porous carbon, the method does not need to carry out acid washing and water washing on the product for removing the metal impurities, does not introduce oxygen-containing functional groups on the surface of the product, and does not need subsequent high-temperature heat treatment to remove the oxygen-containing functional groups.|[0039] (3) According to the invention, the dried material is graded and then subjected to carbon activation, and the control of the particle size is beneficial to improving the uniformity of heat and mass transfer of particles in a high-temperature process, and is particularly beneficial to the contact control of the particles and an activating agent in an activation process, so that the activation uniformity of a carbon aerogel material product is improved, and the uniformity of the product is ensured.|[0040] (4) The silicon-carbon negative electrode carbon aerogel material products with different specific surface areas, pore volumes, average pore diameters and micropore ratios can be prepared by regulating and controlling the technological parameters, and the market adaptability is strong.|INVENTION MODE|Detailed Description|[0041] In order to describe the present invention, a method for preparing a carbon aerogel material for use as a silicon carbon negative electrode according to the present invention will be described in further detail with reference to the accompanying drawings and examples, but is not limited thereto.|[0042] Example 1|[0043] The invention discloses a preparation method of a carbon aerogel material used as a silicon-carbon anode, which comprises the following steps:|[0044] (1) Sol-gel, namely mixing and dissolving a certain amount of phenolic resin, formaldehyde aqueous solution, potassium hydroxide and pore-forming agent, wherein the molar ratio of the phenolic resin to formaldehyde is 1:2, the molar ratio of the phenolic resin to the potassium hydroxide is 50:1, the pore-forming agent is cetyl trimethyl ammonium bromide, the adding ratio is 2% of the mass of the phenolic resin, and the temperature is kept for 10 hours at 65 ℃ to obtain a gel material. |[0045] (2) Crushing, namely crushing the gel material to obtain the crushed gel material with the particle size distribution D50 of 400 mu m.|[0046] (3) Drying, namely placing the crushed gel material into drying equipment for drying, and obtaining the dried material after 15 hours at 90 ℃.|[0047] (4) Classifying, namely classifying the dried material by classifying equipment to obtain classified material, wherein the particle size distribution D50 of the classified material is 400 mu m, and the ratio of (D90-D10)/D50 is less than or equal to 1.2.|[0048] (5) Carbonizing, namely preserving heat for 3 hours at 700 ℃ and carbonizing the grading material by taking nitrogen as a protective gas to obtain a carbonized material.|[0049] (6) Activating, namely activating the carbonized material at 800 ℃ for 8 hours by taking carbon dioxide as an activating agent to obtain an activated material.|[0050] (7) And (3) impurity removal, namely removing iron impurities from the activated material through magnetic separation equipment to obtain an impurity-removed material.|[0051] (8) Grinding, namely further crushing the impurity-removed material, wherein the grinding frequency is 35Hz, and obtaining the carbon aerogel material finished product with the particle size distribution meeting the requirement.|[0052] Examples 2 to 6|[0053] Examples 2-4 steps for preparing carbon aerogel materials for use as silicon carbon anodes the steps and their process parameters were the same as in example 1 except that the activation temperature and time in the activation of step (6) were different from those in example 1. Examples 5-6 steps for preparing carbon aerogel materials for use as silicon carbon anodes the steps and their process parameters were the same as in example 1, except that the ratio of pore-forming agent addition in the sol-gel of step (1) and the activation temperature and time in the activation of step (6) were different from those in example 1. The technical parameters used in examples 2-6 are shown in Table 1.|[0054] Table 1 examples 2-6 technical parameters for preparing carbon aerogel materials for silicon carbon negative electrodes|[0055] |[0056] Performance testing|[0057] The invention tests the performance of the prepared carbon aerogel material, tests the specific surface area, pore volume, average grain diameter and micropore ratio of the carbon aerogel material by using a static method specific surface area and pore diameter analyzer, tests ash content of the carbon aerogel material by using a muffle furnace, tests pH value of the carbon aerogel material by using a pH meter, tests water content of the carbon aerogel material by using a water content meter, tests grain diameter distribution of the carbon aerogel material by using a grain size analyzer, and tests impurity iron element content of the carbon aerogel material by using ICP equipment. The results of the performance test of the carbon aerogel materials prepared in examples 1 to 6 are shown in Table 2.|[0058] TABLE 2 Performance data sheets for carbon aerogel materials prepared in examples 1-6|[0059] |[0060] |[0061] As can be seen from Table 2, the specific surface area and pore volume of the carbon aerogel material can be controlled conveniently by changing the activation temperature and time in examples 1-4, and the control effect of the specific surface area and pore volume is also good by changing the addition of pore-forming agent in examples 4-6 and adjusting the activation time in a small amplitude. (CN117163943)|TECHNICAL FIELD|Technical Field|[0001] The invention belongs to the technical field of preparation of lithium ion battery materials, and particularly relates to a preparation method of a porous carbon matrix material of a silicon-carbon negative electrode.|BACKGROUND ART|[0002] Lithium ion batteries have been rapidly developed since the 70 s of the 20 th century, have the characteristics of high energy density, long cycle life and the like, and have been widely applied to the fields of portable electronic devices, vehicles, energy storage power stations and the like, particularly in the field of new energy automobiles, and have been in great demand in recent years. Along with the increasing demands of people on higher endurance mileage, shorter charging time and the like of new energy automobiles, higher demands are also put forward on the energy density of lithium batteries. Currently, in various lithium ion battery anode materials, graphite anode occupies the main market, but the theoretical capacity of graphite is only 372mAh/g, so that the requirement of higher energy density is difficult to meet, and a novel anode material needs to be developed.|[0003] The inorganic silicon material has the advantages of high earth element abundance, good safety, easy industrialization and the like. As a lithium battery anode material, the huge theoretical specific capacity (4200 mAh/g) of the lithium battery anode material has the unique advantage of preparing a high-performance anode material. However, when silicon is charged and discharged, the silicon material is pulverized in the circulation process due to the huge volume change effect (> 300%), so that various performances of the battery are deteriorated. In addition, silicon is a common semiconductor material, and has poor conductive performance, so that the cycle performance of the silicon anode material in a lithium ion battery is affected.|[0004] In recent years, in order to utilize the high specific capacity of silicon and suppress the volume expansion effect thereof, researchers have conducted a great deal of research, and among them, a preferred technical route is to prepare a silicon/carbon composite material while utilizing the high specific capacity of silicon and good mechanical properties and electrical conductivity of the carbon material.|[0005] Chinese patent CN110098380A discloses a preparation method of a silicon-based negative electrode material of a lithium ion battery, which comprises the steps of firstly etching the surface of a carbon material by adopting a physical or chemical method, forming a plurality of nano-to micron-sized holes on the surface of the carbon material, then carrying out mixed ball milling on the prepared carbon material with the holes and nano-silicon with a certain proportion, embedding the nano-silicon into the holes of the carbon material, and finally carrying out carbon coating treatment on the material after mixed ball milling to obtain the silicon-based negative electrode material of the lithium ion battery. In the method, commercial nano silicon is used as a raw material, the cost is high, in addition, only some holes are formed on the surface of the carbon material, nano silicon particles which can be embedded are limited, and the nano silicon particles are difficult to uniformly enter the pores of the carbon material, so that the excellent performance of the silicon-carbon material cannot be fully exerted. Obviously, the carbon material with high porosity and reasonable pore structure distribution is the basis for the performance of the silicon-carbon anode material. The carbon aerogel has the excellent properties of high porosity, adjustable pore structure and the like, and has great application potential in the field of silicon-carbon cathodes.|[0006] In terms of a preparation method of carbon aerogel, chinese patent CN1895770a discloses a "preparation method of carbon aerogel powder", in which resorcinol-formaldehyde solution containing a certain concentration and a catalyst proportion is uniformly dispersed in an oil phase under the action of ultrasonic wave and at low temperature, and gel polymerization reaction is performed under heating and ultrasonic wave, and organic aerogel powder is obtained through separation and cleaning, and then carbon aerogel powder is obtained through carbon activation. The method uses resorcinol as the raw material, has high cost, can generate a large amount of organic oil to be treated in the production process, has complex process and is not beneficial to large-scale production.|[0007] In conclusion, whether the carbon aerogel material with high purity and reasonable pore structure distribution can be prepared by using a simpler process is a key for improving the performance of the silicon-carbon negative electrode material.|DISCLOSURE|Disclosure of Invention|[0008] The invention aims to solve the problems of complex process, high production cost, low porosity, unreasonable pore structure distribution, poor product consistency, low purity and difficult mass production in the prior art, and provides a preparation method of a carbon aerogel material used as a silicon-carbon negative electrode, wherein the preparation method has the advantages of wide raw material source, simple production process, high product purity, reasonable pore size and reasonable distribution.|[0009] In order to achieve the above purpose, the preparation method of the carbon aerogel material used as the silicon-carbon negative electrode adopts phenolic resin as a main raw material, and the pore structure distribution of the carbon aerogel is adjusted through the steps of sol-gel, crushing, drying, grading, carbon activation, impurity removal, grinding and the like, so that the use requirement of the silicon-carbon negative electrode field on the carbon aerogel is met. The method specifically comprises the following process and steps:|[0010] 1) Sol-gel, namely mixing and dissolving a set amount of phenolic resin, formaldehyde aqueous solution, potassium hydroxide and pore-forming agent, and preserving heat for a period of time at a certain temperature T1 to obtain gel material; |[0011] In the step, the molar ratio of the phenolic resin to formaldehyde is generally 1:1-3.5, preferably 1:1.5-2.5, the molar ratio of the phenolic resin to potassium hydroxide is generally 10-200:1, preferably 40-80:1, the pore-forming agent is preferably cetyl trimethyl ammonium bromide, and the addition ratio of the pore-forming agent is generally 1-10% of the mass of the phenolic resin, preferably 1.5-4.0%; |[0012] In the step, the temperature T1 is 60-80 ℃, and the heat preservation time is 5-15 h. |[0013] 2) Crushing, namely crushing the gel material to obtain fine particle gel material with certain particle size distribution, wherein the D50 of the fine particle gel material is controlled within the range of 100-600 mu m, and preferably 300-600 mu m.|[0014] 3) Drying, namely placing the fine-particle gel material into drying equipment for drying, and obtaining a dried material after a period of time at a certain temperature T2;|[0015] in the step, the temperature T2 is preferably 80-150 ℃, preferably 85-95 ℃, the drying time is 10-20 h, and the moisture content of the dried material is controlled to be less than or equal to 1%. |[0016] 4) Classifying, namely classifying the dried material by classifying equipment to obtain classified material, wherein the granularity D50 of the classified material is controlled to be 300-500 mu m, and the (D90-D10)/D50 is less than or equal to 1.5;|[0017] In this step, D50 is preferably in the range of 400 to 500 μm, and (D90-D10)/D50 is preferably not more than 1.2. |[0018] 5) Carbonizing, namely carbonizing the grading material under the protection of certain carbonization temperature, time and inert gas to obtain carbonized material, wherein the carbonization temperature is controlled in the range of 600-1000 ℃;|[0019] The carbonization time is 2-4h, the carbonization temperature is controlled within the range of 650-800 ℃, the inert atmosphere is one or a mixture of two or more of nitrogen, helium or argon, and the cost of the nitrogen is the lowest. |[0020] 6) Activating, namely activating the carbonized material at a certain activation temperature, time and an activating agent atmosphere to obtain an activated material, wherein the activating agent is one or a mixture of water vapor and carbon dioxide, and the activation temperature is controlled to be 700-1000 ℃;|[0021] In the step, the activation time is controlled to be 6-15 h, preferably 7-10 h, and the activation temperature is controlled to be 750-850 ℃. |[0022] 7) Removing impurities, namely removing iron impurities from the activated material through magnetic separation equipment to obtain a pure material;|[0023] in the step, the selected magnetic separation equipment is preferably dry magnetic separation equipment, such as a Chinese patent ZL201610978391.3 'a dry iron removal device for hollow glass beads', and the magnetic field intensity of the magnetic separation equipment is controlled to ensure that the iron content of the pure material is less than or equal to 100ppm. |[0024] 8) Grinding, namely carrying out further grinding treatment on the pure material to obtain a carbon aerogel material finished product with the specific surface area of 1000-3000 m 2/g, the pore volume of 0.3-2 cm 3/g, the average pore diameter of 0.5-10 nm and the micropore ratio of less than 2 nanometers of 30% -100%.|[0025] In the step 8), equipment adopted in the grinding operation is a vibration grinding machine or a high-speed centrifugal grinding machine, the frequency is 20-45 Hz, 30-40 Hz is preferred, and the particle size distribution D50 of the carbon aerogel material finished product is 2-15 mu m.|[0026] Experimental study shows that the carbon aerogel material finished product with the following product performances can be obtained by controlling the technological parameters of each step:|[0027] ① The specific surface area is 1000-3000 m 2/g, the pore volume is 0.3-2 cm 3/g, the average pore diameter is 0.5-10 nm, and the micropore ratio is 30% -100%; |[0028] ② The specific surface area is 1100-2400 m 2/g, the pore volume is 0.4-1.5 cm 3/g, the average pore diameter is 1.5-3 nm, and the micropore ratio is 60% -100%; |[0029] ③ The specific surface area is 1150-640 m 2/g, the pore volume is 0.45-0.60 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0030] ④ The specific surface area is 1350-1550 m 2/g, the pore volume is 0.55-0.70 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0031] ⑤ The specific surface area is 1550-1750 m 2/g, the pore volume is 0.65-0.80 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0032] ⑥ The specific surface area is 1750-1950 m 2/g, the pore volume is 0.75-0.90 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0033] ⑦ The specific surface area is 1950-2150 m 2/g, the pore volume is 0.85-1.00 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%; |[0034] ⑧ The specific surface area is 2150-2350 m 2/g, the pore volume is 0.95-1.10 cm 3/g, the average pore diameter is 1.5-2.5 nm, and the micropore ratio is 80% -100%. |[0035] Micropores herein refer to pores of less than 2 nanometers.|[0036] Compared with the prior art, the preparation method of the carbon aerogel material used as the silicon-carbon negative electrode has the following advantages:|[0037] (1) The invention uses phenolic resin, formaldehyde, potassium hydroxide and the like as main raw materials, has wide raw material sources, low cost, relatively simple preparation process and high production efficiency, and is suitable for reference in large-scale industrial production. |[0038] (2) Compared with the traditional process for preparing the porous carbon, the method does not need to carry out acid washing and water washing on the product for removing the metal impurities, does not introduce oxygen-containing functional groups on the surface of the product, and does not need subsequent high-temperature heat treatment to remove the oxygen-containing functional groups.|[0039] (3) According to the invention, the dried material is graded and then subjected to carbon activation, and the control of the particle size is beneficial to improving the uniformity of heat and mass transfer of particles in a high-temperature process, and is particularly beneficial to the contact control of the particles and an activating agent in an activation process, so that the activation uniformity of a carbon aerogel material product is improved, and the uniformity of the product is ensured.|[0040] (4) The silicon-carbon negative electrode carbon aerogel material products with different specific surface areas, pore volumes, average pore diameters and micropore ratios can be prepared by regulating and controlling the technological parameters, and the market adaptability is strong.|INVENTION MODE|Detailed Description|[0041] In order to describe the present invention, a method for preparing a carbon aerogel material for use as a silicon carbon negative electrode according to the present invention will be described in further detail with reference to the accompanying drawings and examples, but is not limited thereto.|[0042] Example 1|[0043] The invention discloses a preparation method of a carbon aerogel material used as a silicon-carbon anode, which comprises the following steps:|[0044] (1) Sol-gel, namely mixing and dissolving a certain amount of phenolic resin, formaldehyde aqueous solution, potassium hydroxide and pore-forming agent, wherein the molar ratio of the phenolic resin to formaldehyde is 1:2, the molar ratio of the phenolic resin to the potassium hydroxide is 50:1, the pore-forming agent is cetyl trimethyl ammonium bromide, the adding ratio is 2% of the mass of the phenolic resin, and the temperature is kept for 10 hours at 65 ℃ to obtain a gel material. |[0045] (2) Crushing, namely crushing the gel material to obtain the crushed gel material with the particle size distribution D50 of 400 mu m.|[0046] (3) Drying, namely placing the crushed gel material into drying equipment for drying, and obtaining the dried material after 15 hours at 90 ℃.|[0047] (4) Classifying, namely classifying the dried material by classifying equipment to obtain classified material, wherein the particle size distribution D50 of the classified material is 400 mu m, and the ratio of (D90-D10)/D50 is less than or equal to 1.2.|[0048] (5) Carbonizing, namely preserving heat for 3 hours at 700 ℃ and carbonizing the grading material by taking nitrogen as a protective gas to obtain a carbonized material.|[0049] (6) Activating, namely activating the carbonized material at 800 ℃ for 8 hours by taking carbon dioxide as an activating agent to obtain an activated material.|[0050] (7) And (3) impurity removal, namely removing iron impurities from the activated material through magnetic separation equipment to obtain an impurity-removed material.|[0051] (8) Grinding, namely further crushing the impurity-removed material, wherein the grinding frequency is 35Hz, and obtaining the carbon aerogel material finished product with the particle size distribution meeting the requirement.|[0052] Examples 2 to 6|[0053] Examples 2-4 steps for preparing carbon aerogel materials for use as silicon carbon anodes the steps and their process parameters were the same as in example 1 except that the activation temperature and time in the activation of step (6) were different from those in example 1. Examples 5-6 steps for preparing carbon aerogel materials for use as silicon carbon anodes the steps and their process parameters were the same as in example 1, except that the ratio of pore-forming agent addition in the sol-gel of step (1) and the activation temperature and time in the activation of step (6) were different from those in example 1. The technical parameters used in examples 2-6 are shown in Table 1.|[0054] Table 1 examples 2-6 technical parameters for preparing carbon aerogel materials for silicon carbon negative electrodes|[0055] |[0056] Performance testing|[0057] The invention tests the performance of the prepared carbon aerogel material, tests the specific surface area, pore volume, average grain diameter and micropore ratio of the carbon aerogel material by using a static method specific surface area and pore diameter analyzer, tests ash content of the carbon aerogel material by using a muffle furnace, tests pH value of the carbon aerogel material by using a pH meter, tests water content of the carbon aerogel material by using a water content meter, tests grain diameter distribution of the carbon aerogel material by using a grain size analyzer, and tests impurity iron element content of the carbon aerogel material by using ICP equipment. The results of the performance test of the carbon aerogel materials prepared in examples 1 to 6 are shown in Table 2.|[0058] TABLE 2 Performance data sheets for carbon aerogel materials prepared in examples 1-6|[0059] |[0060] |[0061] As can be seen from Table 2, the specific surface area and pore volume of the carbon aerogel material can be controlled conveniently by changing the activation temperature and time in examples 1-4, and the control effect of the specific surface area and pore volume is also good by changing the addition of pore-forming agent in examples 4-6 and adjusting the activation time in a small amplitude. Family Number|(107609891)|107609891|Abstract|(CN117163943B B)|The invention discloses a preparation method of a carbon aerogel material used as a silicon - carbon negative electrode , which comprises the following steps : by taking phenolic resin as a main raw material , carrying out sol - gel treatment , crushing , drying , grading , carbon activation , impurity removal , grinding and the like , adjusting the pore structure distribution of carbon aerogel , and controlling the indexes such as impurity content , ash content , water content , particle size distribution and the like , so as to prepare the carbon aerogel material used as the silicon - carbon negative electrode . The use requirements of the silicon - carbon negative electrode field on the carbon aerogel are met . The prepared carbon aerogel material has a specific surface area of 1000-3000 m < 2 > / g , a pore volume of 0.3-2 cm < 3 > / g , an average pore size of 0.5-10 nm and a micropore proportion of 30-100%, and can be used as a porous carbon matrix material of a silicon - carbon negative electrode . Phenolic resin , formaldehyde , potassium hydroxide and the like are used as main raw materials , so that the cost is low ; the material is graded and then subjected to carbon activation , the controllability and consistency of the material in the carbon activation process are guaranteed , meanwhile , the impurity removal technology is simple , the whole technology is efficient , and large - scale production of the carbon aerogel material is facilitated . |IPC codes|(CN117163943B B)|B01J - 013/00 |C01B - 032/05 | Chemical engineering|Electrical machinery, apparatus, energy|Materials, metallurgy B01J-013/00/91|B01J-020/20|C01B-032/00|C01B-032/05|C01P-2002/01|C01P-2002/72|C01P-2002/82|C01P-2004/03|C01P-2004/04|C01P-2004/61|C01P-2004/80|C01P-2006/12|C01P-2006/14|C01P-2006/16|C01P-2006/40|H01M-004/36/6|H01M-004/583|H01M-004/587|H01M-004/62/5|H01M-010/052|H01M-010/0525|Y02E-060/10 B01J-013/00/91|B01J-020/20|C01B-032/00|C01B-032/05|C01P-2002/01|C01P-2002/72|C01P-2002/82|C01P-2004/03|C01P-2004/04|C01P-2004/61|C01P-2004/80|C01P-2006/12|C01P-2006/14|C01P-2006/16|C01P-2006/40|H01M-004/36/6|H01M-004/583|H01M-004/587|H01M-004/62/5|H01M-010/052|H01M-010/0525|Y02E-060/10 B01J-013/00|C01B-032/05|H01M-004/38|H01M-004/587 B01J-013/00|C01B-032/05|H01M-004/38|H01M-004/587 CN116314644|WO202207401|WO201895285|CN1583555|US5744510|CN116102010|CN108147389 CN116314644 105521023 WHO=Examiner SELF=Y CAT=A|WO202207401 90949313 WHO=Examiner SELF=N CAT=A|WO201895285 79885062 WHO=Examiner SELF=N CAT=A|CN1583555 61931832 WHO=Examiner SELF=N CAT=A|US5744510 43001637 WHO=Examiner SELF=N CAT=A|CN116102010 104929319 WHO=Examiner SELF=N|CN108147389 80011394 WHO=Examiner SELF=N LI, LL等: &quot;&quot;Mechanical and thermal insulation properties of carbon fibre-reinforced carbon aerogel composites&quot;&quot;, 《 ADVANCES IN APPLIED CERAMICS》, vol. 121, no. 5, 27 December 2022 (2022-12-27), pages 222 - 230 (Cat. A)|贾献峰等: &quot;“常压干燥制备酚醛树脂基炭气凝胶研究进展”&quot;, 《化学通报》, vol. 84, no. 03, 31 December 2021 (2021-12-31), pages 194 - 203 (Cat. A) US5744510; CN1583555; WO201895285; WO202207401; CN116314644; CN108147389; CN116102010 GRANTED (CN117163943)|GRANTED ALIVE (CN117163943)|ALIVE (CN117163943)|LEGAL DETAILS FOR CN117163943|Actual or expected expiration date=2043-09-14|Legal state=ALIVE|Status=GRANTED|Event publication date=2023-09-14|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202311184117|Application date=2023-09-14|Standardized application number=2023CN-1184117|Event publication date=2023-12-05|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN117163943|Publication stage code=A|Publication date=2023-12-05|Standardized publication number=CN117163943|Event publication date=2023-12-05|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-12-22|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2025-09-12|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN117163943|Publication stage code=B|Publication date=2025-09-12|Standardized publication number=CN117163943B|Event publication date=2025-09-12|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN117163943)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTHrHKnQMfN0Bj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000078926372&ekey=2157&xpn=CN117163943B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=By5hqJ%252BaVi%252Fp9QfaShXbirmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN117163943)|CN|(CN117163943)|CN (CN117163943)|NAME=SINOSTEEL MAANSHAN GENERAL INSTITUTE OF MINING RESEARCH CO., LTD , COUNTRY=CN|(CN117163943)|NAME=SINOSTEEL MAANSHAN GENERAL INSTITUTE OF MINING RESEARCH CO., LTD , COUNTRY=CN (CN117163943)|NAME=CHANG QIANFA;MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. , REG=34111NAME=XI ZHIPENG;MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. , REG=34111|(CN117163943)|NAME=CHANG QIANFA;MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. , REG=34111NAME=XI ZHIPENG;MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. MA'ANSHAN CITY JINQIAO PATENT AGENT LTD. , REG=34111 (CN117163943)|CN| (CN117163943)|NAME=WANG JUN, COUNTRY=CN |NAME=JIN LIANG|NAME=PAN ZHE|NAME=LIU YAHUI|(CN117163943)|NAME=WANG JUN|NAME=JIN LIANG|NAME=PAN ZHE|NAME=LIU YAHUI 0 1 Titre: (CN117163943)|Preparation method of carbon aerogel material used as silicon-carbon negative electrode Résumé: (CN117163943)|The invention discloses a preparation method of a carbon aerogel material used as a silicon-carbon negative electrode, which comprises the following steps: by taking phenolic resin as a main raw material, carrying out sol-gel treatment, crushing, drying, grading, carbon activation, impurity removal, grinding and the like, adjusting the pore structure distribution of carbon aerogel, and controlling the indexes such as impurity content, ash content, water content, particle size distribution and the like, so as to prepare the carbon aerogel material used as the silicon-carbon negative electrode. The use requirements of the silicon-carbon negative electrode field on the carbon aerogel are met. The prepared carbon aerogel material has a specific surface area of 1000-3000 m < 2 >/g, a pore volume of 0.3-2 cm < 3 >/g, an average pore size of 0.5-10 nm and a micropore proportion of 30-100%, and can be used as a porous carbon matrix material of a silicon-carbon negative electrode. Phenolic resin, formaldehyde, potassium hydroxide and the like are used as main raw materials, so that the cost is low; the material is graded and then subjected to carbon activation, the controllability and consistency of the material in the carbon activation process are guaranteed, meanwhile, the impurity removal technology is simple, the whole technology is efficient, and large-scale production of the carbon aerogel material is facilitated. 120 Abstract gpt-4o-mini no The article focuses on the preparation of carbon aerogel materials for use in silicon-carbon negative electrodes, which does not relate to accelerated weathering or CO₂ capture.
119 CN202010572825 CN202010572825 CN111672470 90688200 CN111672470 A 2020-09-18 [CN111672470] 2020-06-22 2020-06-22 2020-09-18 (CN111672470)|2022-11-15 (CN111672470)|Preparation method of charcoal for phosphorus removal (CN111672470)|The invention discloses a preparation method of charcoal for phosphorus removal. The preparation method mainly comprises the following steps: mixing dried and crushed sludge with eggshell powder, andcarrying out anaerobic pyrolysis treatment. The invention also discloses a use method of the biological carbon for phosphorus removal. According to the preparation method of the charcoal for phosphorus removal, provided by the invention, municipal residual sludge and waste eggshells are mixed and pyrolyzed to prepare the charcoal, so that resource utilization of wastes is realized, and the problems of relatively low sludge recycling rate, large sludge volume and environmental pollution caused by spoilage at present can be solved to a great extent. The raw materials are rich in source, easy toobtain and low in cost, the method is simple and feasible, and the prepared charcoal has a remarkable and stable removal effect on phosphorus in sewage and wastewater. TIANJIN UNIVERSITY OF SCIENCE & TECHNOLOGY (CN111672470)|TIANJIN UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) LI GUIJU|CHEN WENTAO (CN111672470)|LI GUIJU|CHEN WENTAO (CN111672470)|WANG XIAN;TIANJIN CAIZHI PATENT&TRADEMARK AGENCY, LTD.|Reg. Nb: 12108 (CN111672470)|The method has the advantages of rich raw material sources, easy acquisition, low cost, simplicity and feasibility, and the prepared biochar has obvious and stable effect on removing phosphorus in sewage and wastewater.|According to the preparation method of the biochar for removing phosphorus, provided by the invention, the biochar is prepared by mixing and pyrolyzing the urban excess sludge and the waste eggshells, so that the resource utilization of wastes is realized, and the problems of low sludge recycling rate, large sludge volume and environmental pollution caused by putrefaction and deterioration can be solved to a great extent.|Among them, chemical and biological treatments have many disadvantages such as side reactions, by-products, pretreatment, etc., and adsorption treatment is considered as one of more economical and effective methods.|On the other hand, phosphorus is a limited resource as a factor limiting plant growth.| (CN111672470)|1. A preparation method of biochar for phosphorus removal is characterized by comprising the following steps:1) drying, crushing and sieving the sludge to obtain sludge powder;2) cleaning eggshells, drying, crushing and sieving to obtain eggshell powder;3) and fully mixing the sludge powder and the eggshell powder, and then carrying out anaerobic pyrolysis to obtain a product after pyrolysis treatment.| (CN111672470)|In addition, the invention also provides a using method of the biochar.|The invention discloses a preparation method of biochar for phosphorus removal, which mainly comprises the following steps: mixing the dried and crushed sludge and the eggshell powder and carrying out anaerobic pyrolysis treatment. The invention also discloses a use method of the biochar for removing phosphorus.|the invention relates to the field of solid waste resource utilization, in particular to a preparation method and an application method of biochar for phosphorus removal.| (CN111672470)|PHOSPHORUS REMOVAL(100,34)|BIOCHAR(100,31)|EGGSHELL POWDER(99,10)|ANAEROBIC PYROLYSIS(94,11)|ANAEROBIC PYROLYSIS TREATMENT(79,1)|SLUDGE POWDER(77,11)|CRUSHED SLUDGE(67,1)|RESOURCE UTILIZATION(61,2)|DRIED SLUDGE(61,1)|ANAEROBIC PYROLYSIS TEMPERATURE(59,6)|CLEANING EGGSHELL(50,2)|WASTE EGGSHELL(44,1)|SOLID WASTE RESOURCE UTILIZATION(31,1)|GEL SUBSTANCE(30,10)|PYROLYSIS TREATMENT(30,5)|CRUSHING(28,10)|PREPARED BIOCHAR(25,2)|PUTREFACTION(24,1)|ACQUISITION(23,1)|FEASIBILITY(22,1)|DEWATERED URBAN EXCESS SLUDGE(20,3)|SCREEN(20,2)|SLUDGE RECYCLING RATE(20,1)|DETERIORATION(19,1)|ENVIRONMENTAL POLLUTION(19,1)|SLUDGE(18,6)|SEWAGE(18,1)|MIXED SLURRY(16,5)|DRYING TEMPERATURE(15,1)|SIMULATED WASTEWATER(14,3)|LARGE SLUDGE VOLUME(12,1)|SOLID WASTE(11,1)|CLEANING WASTE EGG SHELL(10,3)|MIXING SLUDGE POWDER(10,3)|PHOSPHORUS ORE(10,2)|BIOCHAR PRODUCT(9,4)|PHOSPHORUS CONCENTRATION CONTENT RANGE(9,2)|CHICKEN EGGSHELL(9,1)|CLEANED WASTE(8,3)|DEWATERED SLUDGE(8,1)|WET SLUDGE CAKE(8,1)|MASS RATIO(7,6)|CONSTANT TEMPERATURE(6,5)|DEIONIZED WATER(6,5)|CRUCIBLE(6,3)|PYROLYSIS TEMPERATURE(6,3)|RICH RAW MATERIAL SOURCE(6,1)|URBANIZATION RAPID DEVELOPMENT(6,1)|ADSORPTION CAPACITY MEASUREMENT(5,1)|ANIMAL HUSBANDRY DEVELOPMENT(5,1)|DRY SLUDGE(5,1)|SLUDGE FULL UTILIZATION(5,1)|ROOM TEMPERATURE(4,5)|ROTATING SPEED(4,3)|BACTERIAL CELL(4,1)|ORGANIC CONTAMINANT(4,1)|STABILIZATION TREATMENT(4,1)| (CN111672470)|1. A preparation method of biochar for phosphorus removal is characterized by comprising the following steps:|1) drying, crushing and sieving the sludge to obtain sludge powder;|2) cleaning eggshells, drying, crushing and sieving to obtain eggshell powder;|3) and fully mixing the sludge powder and the eggshell powder, and then carrying out anaerobic pyrolysis to obtain a product after pyrolysis treatment.|2. The method for preparing biochar for phosphorus removal according to claim 1, which is characterized in that: in the step 3), the sludge powder and the eggshell powder are mixed according to the mass ratio of 1: 1-3, mixing; the temperature of the anaerobic pyrolysis is 700-900 ℃, and the retention time is 1.5-2.5 h.|3. The method for preparing biochar for phosphorus removal according to claim 2, which is characterized in that: the temperature of the anaerobic pyrolysis in the step 3) is 900 ℃.|4. The method for preparing biochar for phosphorus removal according to any one of claims 1 to 3, which is characterized in that: the sludge powder and the eggshell powder are mixed in the step 3) in the following way: adding a mixture of sludge powder and eggshell powder into a proper amount of deionized water, and stirring at room temperature for 6-12 h; and then, continuously stirring the mixed slurry at 60-80 ℃ for 2-4 h to obtain a gel substance, and drying the obtained gel substance at 90-105 ℃ for at least 12 h.|5. The method for preparing biochar for phosphorus removal according to any one of claims 1 to 3, which is characterized in that: in the step 1) and the step 2), the mesh number of the screened screen is 100-300 meshes, and the drying temperature is 80-105 ℃; in the step 2), the eggshell is selected from the eggshells with calcium carbonate content higher than 94 wt%.|6. The use method of the biochar for removing phosphorus prepared by the method of claim 1 is characterized in that: determining the adding amount of the biochar for removing phosphorus according to the phosphorus concentration content range in the wastewater: when the phosphorus concentration in the wastewater is lower than 50mg/L, the adding amount of the biochar for removing phosphorus is 1-1.5 g/L; when the phosphorus concentration in the wastewater is 50-200 mg/L, the adding amount of the biochar for removing phosphorus is 2-3 g/L; stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|7. The use method of biochar for phosphorus removal according to claim 6, which is characterized in that: in the step 3), the sludge powder and the eggshell powder are mixed according to the mass ratio of 1: 1-3, mixing; the temperature of the anaerobic pyrolysis is 700-900 ℃, and the retention time is 1.5-2.5 h.|8. The use method of biochar for phosphorus removal according to claim 7, which is characterized in that: the temperature of the anaerobic pyrolysis in the step 3) is 900 ℃. (CN111672470)|TECHNICAL FIELD|[0001] The technical field is as follows:|[0002] the invention relates to the field of solid waste resource utilization, in particular to a preparation method and an application method of biochar for phosphorus removal.|BACKGROUND ART|[0004] since nearly two centuries, the concentration of phosphate in lakes and rivers in the world has increased significantly due to human activities, the development of animal husbandry, the widespread use of phosphate, and the direct discharge of phosphate in water, thereby causing eutrophication and destruction of the ecosystem. On the other hand, phosphorus is a limited resource as a factor limiting plant growth. Phosphorus ore is the main phosphorus source of phosphate fertilizer, and the storage amount of phosphorus ore in the world is estimated to be between 30 and 300 years at present.|[0005] Different phosphorus removal technologies have been developed and applied worldwide, such as chemical phosphorus removal, biological phosphorus removal, and physical phosphorus removal. Among them, chemical and biological treatments have many disadvantages such as side reactions, by-products, pretreatment, etc., and adsorption treatment is considered as one of more economical and effective methods.|[0006] Sludge is an inevitable by-product in the sewage treatment process, along with the rapid development of urbanization, a large amount of urban excess sludge is produced worldwide, and the urban excess sludge mainly comprises various inorganic and organic components, including: SiO 22、CaO、Al2O3MgO, various transition metals (Fe, Ni, Co and other species), bacterial cells, biological macromolecules and organic contaminants, generally considered as contaminants. The total amount of the urban excess sludge is on the increasing trend, and the annual output of wet sludge cakes in China is estimated to be more than 6000 million (calculated by the water content of 80%) and the dry sludge amount is estimated to be 1200 million by 2020-2025. In this context, about 80% of the dewatered sludge is still secondary polluted by direct landfill or incineration without stabilization treatment, so the treatment and disposal of the sludge has become a problem.|DISCLOSURE|[0007] The invention content is as follows:|[0008] aiming at the defects and shortcomings that the existing sludge treatment technology cannot realize the full utilization of sludge and the increasingly serious problem of water environment phosphorus pollution, the invention aims to provide a method for preparing biochar by fully utilizing urban excess sludge, and the prepared biochar is low in price and stable and is specially used for removing the phosphorus pollution of a water body. In addition, the invention also provides a using method of the biochar.|[0009] The technical scheme of the invention is as follows:|[0010] a preparation method of biochar for phosphorus removal specifically comprises the following steps:|[0011] 1) drying, crushing and sieving the sludge to obtain sludge powder;|[0012] 2) cleaning eggshells, drying, crushing and sieving to obtain eggshell powder;|[0013] 3) and fully mixing the sludge powder and the eggshell powder, and then carrying out anaerobic pyrolysis to obtain a product after pyrolysis treatment.|[0014] Further, in the step 3), the sludge powder and the eggshell powder are mixed according to a mass ratio of 1: 1-3, mixing; the temperature of the anaerobic pyrolysis is 700-900 ℃, and the retention time is 1.5-2.5 h.|[0015] Preferably, the temperature of the anaerobic pyrolysis in the step 3) is 900 ℃.|[0016] Further, in the step 3), the sludge powder and the eggshell powder are mixed in the following manner: adding a mixture of sludge powder and eggshell powder into a proper amount of deionized water, and stirring at room temperature for 6-12 h; and then, continuously stirring the mixed slurry at 60-80 ℃ for 2-4 h to obtain a gel substance, and drying the obtained gel substance at 90-105 ℃ for at least 12 h.|[0017] Further, the mesh number of the screen subjected to sieving treatment in the step 1) and the step 2) is 100-300 meshes; the temperature of the drying treatment in the step 1) and the step 2) is 80-105 ℃.|[0018] Further, in the step 2), the eggshell is selected from eggshells with calcium carbonate content higher than 94 wt%, such as eggshells of chicken, duck, etc.|[0019] On the basis, the invention further provides a using method of the biochar for removing phosphorus, which is characterized by comprising the following steps:|[0020] 1) determining the adding amount of the biochar for removing phosphorus according to the phosphorus concentration content range in the wastewater: when the phosphorus concentration in the wastewater is lower than 50mg/L, the adding amount of the biochar for removing phosphorus is 1-1.5 g/L; when the phosphorus concentration in the wastewater is 50-200 mg/L, the adding amount of the biochar for removing phosphorus is 2-3 g/L;|[0021] 2) stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|[0022] According to the preparation method of the biochar for removing phosphorus, provided by the invention, the biochar is prepared by mixing and pyrolyzing the urban excess sludge and the waste eggshells, so that the resource utilization of wastes is realized, and the problems of low sludge recycling rate, large sludge volume and environmental pollution caused by putrefaction and deterioration can be solved to a great extent. The method has the advantages of rich raw material sources, easy acquisition, low cost, simplicity and feasibility, and the prepared biochar has obvious and stable effect on removing phosphorus in sewage and wastewater.|INVENTION MODE|[0023] Detailed Description|[0024] The technical scheme and technical effects of the present invention are further described below with reference to specific embodiments.|INVENTION MODE|[0025] Example 1|[0026] 1) Drying the dewatered urban excess sludge at 105 ℃, then crushing, and sieving by a 100-mesh sieve to obtain sludge powder with the particle size of about 150 mu m;|[0027] 2) cleaning waste egg shells, drying at 105 ℃, crushing, and sieving with a 100-mesh sieve to obtain egg shell powder with the particle size of about 150 mu m;|[0028] 3) mixing sludge powder and eggshell powder according to a mass ratio of 1: 1, fully mixing, wherein the mixing process is as follows: adding the mixture of the two powders into a proper amount of deionized water, and stirring at the room temperature at the rotating speed of 120rpm for 12 hours; and then, continuously stirring the mixed slurry at 80 ℃ for 3h to obtain a gel substance, and drying the obtained gel substance at 105 ℃ for 12 h.|[0029] 4) And (3) carrying out anaerobic pyrolysis on the dried mixture in a crucible, wherein the pyrolysis temperature is 800 ℃, the retention time is 2h, and obtaining a biochar product A for removing phosphorus after the pyrolysis treatment.|[0030] Simulated wastewater with the phosphorus concentration of 5mg/L is treated by the biochar for phosphorus removal prepared in example 1, and the adding amount of the biochar for phosphorus removal is 1.0 g/L. Stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|[0031] The determination result shows that the phosphorus concentration in the wastewater treated by the biochar for phosphorus removal is reduced to 0.06mg/L, and the removal rate reaches 98.78%.|INVENTION MODE|[0032] Example 2|[0033] 1) Drying the dewatered urban excess sludge at 105 ℃, then crushing, and sieving by a 200-mesh sieve to obtain sludge powder with the particle size of about 75 microns;|[0034] 2) cleaning waste egg shells, drying at 105 ℃, crushing, and sieving with a 200-mesh sieve to obtain egg shell powder with the particle size of about 75 mu m;|[0035] 3) mixing sludge powder and eggshell powder according to a mass ratio of 1: 2, fully mixing, wherein the mixing process is as follows: adding the mixture of the two powders into a proper amount of deionized water, and stirring at the room temperature at the rotating speed of 120rpm for 12 hours; and then, continuously stirring the mixed slurry at 80 ℃ for 3h to obtain a gel substance, and drying the obtained gel substance at 105 ℃ for 12 h.|[0036] 4) And (3) carrying out anaerobic pyrolysis on the dried mixture in a crucible, wherein the pyrolysis temperature is 850 ℃, the retention time is 2h, and the biochar product B for removing phosphorus is obtained after pyrolysis treatment.|[0037] The simulated wastewater with the phosphorus concentration of 50mg/L is treated by the biochar for phosphorus removal prepared in example 2, and the adding amount of the biochar for phosphorus removal is 2 g/L. Stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|[0038] The determination result shows that the phosphorus concentration in the wastewater treated by the biochar for phosphorus removal is reduced to 1.91mg/L, and the removal rate reaches 96.18%.|INVENTION MODE|[0039] Example 3|[0040] 1) Drying the dewatered urban excess sludge at 105 ℃, then crushing, and sieving by a 300-mesh sieve to obtain sludge powder with the particle size of about 48 microns;|[0041] 2) cleaning waste egg shells, drying at 105 ℃, crushing, and sieving with a 300-mesh sieve to obtain egg shell powder with the particle size of about 48 mu m;|[0042] 3) mixing sludge powder and eggshell powder according to a mass ratio of 1: 3, fully mixing, wherein the mixing process is as follows: adding the mixture of the two powders into a proper amount of deionized water, and stirring at the room temperature at the rotating speed of 120rpm for 10 hours; and then, continuously stirring the mixed slurry at 70 ℃ for 4h to obtain a gel substance, and drying the obtained gel substance at 105 ℃ for 12 h.|[0043] 4) And (3) carrying out anaerobic pyrolysis on the dried mixture in a crucible, wherein the pyrolysis temperature is 900 ℃, the retention time is 2h, and obtaining a biochar product C for removing phosphorus after the pyrolysis treatment.|[0044] Simulated wastewater with the phosphorus concentration of 200mg/L is treated by the biochar for phosphorus removal prepared in example 3, and the adding amount of the biochar for phosphorus removal is 2 g/L. Stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|[0045] The determination result shows that the phosphorus concentration in the wastewater treated by the biochar for phosphorus removal is reduced to 2.59mg/L, and the removal rate reaches 98.70%.|[0046] Further results of the adsorption capacity measurement are shown in Table 1, the adsorption capacity of the products of 3 examples exceeds 50mg/g, and the adsorption capacity of the product C is 186.81 mg/g.|[0047] TABLE 13 maximum adsorption Capacity of the biochar product obtained in the examples|[0048] (CN111672470)|TECHNICAL FIELD|[0001] The technical field is as follows:|[0002] the invention relates to the field of solid waste resource utilization, in particular to a preparation method and an application method of biochar for phosphorus removal.|BACKGROUND ART|[0004] since nearly two centuries, the concentration of phosphate in lakes and rivers in the world has increased significantly due to human activities, the development of animal husbandry, the widespread use of phosphate, and the direct discharge of phosphate in water, thereby causing eutrophication and destruction of the ecosystem. On the other hand, phosphorus is a limited resource as a factor limiting plant growth. Phosphorus ore is the main phosphorus source of phosphate fertilizer, and the storage amount of phosphorus ore in the world is estimated to be between 30 and 300 years at present.|[0005] Different phosphorus removal technologies have been developed and applied worldwide, such as chemical phosphorus removal, biological phosphorus removal, and physical phosphorus removal. Among them, chemical and biological treatments have many disadvantages such as side reactions, by-products, pretreatment, etc., and adsorption treatment is considered as one of more economical and effective methods.|[0006] Sludge is an inevitable by-product in the sewage treatment process, along with the rapid development of urbanization, a large amount of urban excess sludge is produced worldwide, and the urban excess sludge mainly comprises various inorganic and organic components, including: SiO 22、CaO、Al2O3MgO, various transition metals (Fe, Ni, Co and other species), bacterial cells, biological macromolecules and organic contaminants, generally considered as contaminants. The total amount of the urban excess sludge is on the increasing trend, and the annual output of wet sludge cakes in China is estimated to be more than 6000 million (calculated by the water content of 80%) and the dry sludge amount is estimated to be 1200 million by 2020-2025. In this context, about 80% of the dewatered sludge is still secondary polluted by direct landfill or incineration without stabilization treatment, so the treatment and disposal of the sludge has become a problem.|DISCLOSURE|[0007] The invention content is as follows:|[0008] aiming at the defects and shortcomings that the existing sludge treatment technology cannot realize the full utilization of sludge and the increasingly serious problem of water environment phosphorus pollution, the invention aims to provide a method for preparing biochar by fully utilizing urban excess sludge, and the prepared biochar is low in price and stable and is specially used for removing the phosphorus pollution of a water body. In addition, the invention also provides a using method of the biochar.|[0009] The technical scheme of the invention is as follows:|[0010] a preparation method of biochar for phosphorus removal specifically comprises the following steps:|[0011] 1) drying, crushing and sieving the sludge to obtain sludge powder;|[0012] 2) cleaning eggshells, drying, crushing and sieving to obtain eggshell powder;|[0013] 3) and fully mixing the sludge powder and the eggshell powder, and then carrying out anaerobic pyrolysis to obtain a product after pyrolysis treatment.|[0014] Further, in the step 3), the sludge powder and the eggshell powder are mixed according to a mass ratio of 1: 1-3, mixing; the temperature of the anaerobic pyrolysis is 700-900 ℃, and the retention time is 1.5-2.5 h.|[0015] Preferably, the temperature of the anaerobic pyrolysis in the step 3) is 900 ℃.|[0016] Further, in the step 3), the sludge powder and the eggshell powder are mixed in the following manner: adding a mixture of sludge powder and eggshell powder into a proper amount of deionized water, and stirring at room temperature for 6-12 h; and then, continuously stirring the mixed slurry at 60-80 ℃ for 2-4 h to obtain a gel substance, and drying the obtained gel substance at 90-105 ℃ for at least 12 h.|[0017] Further, the mesh number of the screen subjected to sieving treatment in the step 1) and the step 2) is 100-300 meshes; the temperature of the drying treatment in the step 1) and the step 2) is 80-105 ℃.|[0018] Further, in the step 2), the eggshell is selected from eggshells with calcium carbonate content higher than 94 wt%, such as eggshells of chicken, duck, etc.|[0019] On the basis, the invention further provides a using method of the biochar for removing phosphorus, which is characterized by comprising the following steps:|[0020] 1) determining the adding amount of the biochar for removing phosphorus according to the phosphorus concentration content range in the wastewater: when the phosphorus concentration in the wastewater is lower than 50mg/L, the adding amount of the biochar for removing phosphorus is 1-1.5 g/L; when the phosphorus concentration in the wastewater is 50-200 mg/L, the adding amount of the biochar for removing phosphorus is 2-3 g/L;|[0021] 2) stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|[0022] According to the preparation method of the biochar for removing phosphorus, provided by the invention, the biochar is prepared by mixing and pyrolyzing the urban excess sludge and the waste eggshells, so that the resource utilization of wastes is realized, and the problems of low sludge recycling rate, large sludge volume and environmental pollution caused by putrefaction and deterioration can be solved to a great extent. The method has the advantages of rich raw material sources, easy acquisition, low cost, simplicity and feasibility, and the prepared biochar has obvious and stable effect on removing phosphorus in sewage and wastewater.|INVENTION MODE|[0023] Detailed Description|[0024] The technical scheme and technical effects of the present invention are further described below with reference to specific embodiments.|INVENTION MODE|[0025] Example 1|[0026] 1) Drying the dewatered urban excess sludge at 105 ℃, then crushing, and sieving by a 100-mesh sieve to obtain sludge powder with the particle size of about 150 mu m;|[0027] 2) cleaning waste egg shells, drying at 105 ℃, crushing, and sieving with a 100-mesh sieve to obtain egg shell powder with the particle size of about 150 mu m;|[0028] 3) mixing sludge powder and eggshell powder according to a mass ratio of 1: 1, fully mixing, wherein the mixing process is as follows: adding the mixture of the two powders into a proper amount of deionized water, and stirring at the room temperature at the rotating speed of 120rpm for 12 hours; and then, continuously stirring the mixed slurry at 80 ℃ for 3h to obtain a gel substance, and drying the obtained gel substance at 105 ℃ for 12 h.|[0029] 4) And (3) carrying out anaerobic pyrolysis on the dried mixture in a crucible, wherein the pyrolysis temperature is 800 ℃, the retention time is 2h, and obtaining a biochar product A for removing phosphorus after the pyrolysis treatment.|[0030] Simulated wastewater with the phosphorus concentration of 5mg/L is treated by the biochar for phosphorus removal prepared in example 1, and the adding amount of the biochar for phosphorus removal is 1.0 g/L. Stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|[0031] The determination result shows that the phosphorus concentration in the wastewater treated by the biochar for phosphorus removal is reduced to 0.06mg/L, and the removal rate reaches 98.78%.|INVENTION MODE|[0032] Example 2|[0033] 1) Drying the dewatered urban excess sludge at 105 ℃, then crushing, and sieving by a 200-mesh sieve to obtain sludge powder with the particle size of about 75 microns;|[0034] 2) cleaning waste egg shells, drying at 105 ℃, crushing, and sieving with a 200-mesh sieve to obtain egg shell powder with the particle size of about 75 mu m;|[0035] 3) mixing sludge powder and eggshell powder according to a mass ratio of 1: 2, fully mixing, wherein the mixing process is as follows: adding the mixture of the two powders into a proper amount of deionized water, and stirring at the room temperature at the rotating speed of 120rpm for 12 hours; and then, continuously stirring the mixed slurry at 80 ℃ for 3h to obtain a gel substance, and drying the obtained gel substance at 105 ℃ for 12 h.|[0036] 4) And (3) carrying out anaerobic pyrolysis on the dried mixture in a crucible, wherein the pyrolysis temperature is 850 ℃, the retention time is 2h, and the biochar product B for removing phosphorus is obtained after pyrolysis treatment.|[0037] The simulated wastewater with the phosphorus concentration of 50mg/L is treated by the biochar for phosphorus removal prepared in example 2, and the adding amount of the biochar for phosphorus removal is 2 g/L. Stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|[0038] The determination result shows that the phosphorus concentration in the wastewater treated by the biochar for phosphorus removal is reduced to 1.91mg/L, and the removal rate reaches 96.18%.|INVENTION MODE|[0039] Example 3|[0040] 1) Drying the dewatered urban excess sludge at 105 ℃, then crushing, and sieving by a 300-mesh sieve to obtain sludge powder with the particle size of about 48 microns;|[0041] 2) cleaning waste egg shells, drying at 105 ℃, crushing, and sieving with a 300-mesh sieve to obtain egg shell powder with the particle size of about 48 mu m;|[0042] 3) mixing sludge powder and eggshell powder according to a mass ratio of 1: 3, fully mixing, wherein the mixing process is as follows: adding the mixture of the two powders into a proper amount of deionized water, and stirring at the room temperature at the rotating speed of 120rpm for 10 hours; and then, continuously stirring the mixed slurry at 70 ℃ for 4h to obtain a gel substance, and drying the obtained gel substance at 105 ℃ for 12 h.|[0043] 4) And (3) carrying out anaerobic pyrolysis on the dried mixture in a crucible, wherein the pyrolysis temperature is 900 ℃, the retention time is 2h, and obtaining a biochar product C for removing phosphorus after the pyrolysis treatment.|[0044] Simulated wastewater with the phosphorus concentration of 200mg/L is treated by the biochar for phosphorus removal prepared in example 3, and the adding amount of the biochar for phosphorus removal is 2 g/L. Stirring for 24 hours at the constant temperature of 25 ℃ after the addition is finished.|[0045] The determination result shows that the phosphorus concentration in the wastewater treated by the biochar for phosphorus removal is reduced to 2.59mg/L, and the removal rate reaches 98.70%.|[0046] Further results of the adsorption capacity measurement are shown in Table 1, the adsorption capacity of the products of 3 examples exceeds 50mg/g, and the adsorption capacity of the product C is 186.81 mg/g.|[0047] TABLE 13 maximum adsorption Capacity of the biochar product obtained in the examples|[0048] Family Number|(90688200)|90688200|Abstract|(CN111672470 A)|The invention discloses a preparation method of charcoal for phosphorus removal . The preparation method mainly comprises the following steps : mixing dried and crushed sludge with eggshell powder , andcarrying out anaerobic pyrolysis treatment . The invention also discloses a use method of the biological carbon for phosphorus removal . According to the preparation method of the charcoal for phosphorus removal , provided by the invention , municipal residual sludge and waste eggshells are mixed and pyrolyzed to prepare the charcoal , so that resource utilization of wastes is realized , and the problems of relatively low sludge recycling rate , large sludge volume and environmental pollution caused by spoilage at present can be solved to a great extent . The raw materials are rich in source , easy toobtain and low in cost , the method is simple and feasible , and the prepared charcoal has a remarkable and stable removal effect on phosphorus in sewage and wastewater . |CPC codes|(CN111672470 A)|B01J - 020/20 |B01J - 2220/4887 |IPC codes|(CN111672470 A)|B01J - 020/20 |B01J - 020/30 | Chemical engineering|Environmental technology B01J-020/20|B01J-2220/4887|C02F-001/28/3|C02F-2101/105 B01J-020/20|B01J-2220/4887|C02F-001/28/3|C02F-2101/105 B01J-020/20|B01J-020/30|C02F-001/28|C02F-101/10 B01J-020/20|B01J-020/30|C02F-001/28|C02F-101/10 WO202578845|CN114405472|CN114307956|GB2634563 WO202578845 107630341 WHO=Examiner SELF=N CAT=X CAT=I|CN114405472 99846655 WHO=Examiner SELF=N CAT=A|CN114307956 99529320 WHO=Examiner SELF=N CAT=A|GB2634563 107630341 WHO=Examiner SELF=N CN111135790|CN111253125|US20200023335|CN109012593|CN106902787 CN111135790 88724545 WHO=Examiner SELF=N CAT=A|CN111253125 89186066 WHO=Examiner SELF=N CAT=A|US20200023335 87396214 WHO=Examiner SELF=N CAT=A|CN109012593 82518318 WHO=Examiner SELF=N CAT=A|CN106902787 76644134 WHO=Examiner SELF=N CAT=A LINGJUN KONG等: &quot;Nano-rod Ca-decorated sludge derived carbon for removal of phosphorus&quot;, 《ENVIRONMENTAL POLLUTION》 (Cat. Y)|JIEYANG 等: &quot;Efficient recovery of phosphate from aqueous solution using biochar derived from co-pyrolysis of sewage sludge with eggshell&quot;, 《JOURNAL OF ENVIRONMENTAL CHEMICAL ENGINEERING》 (Cat. T)|XIAONING LIU等: &quot;Adsorption recovery of phosphate from aqueous solution by CaO-biochar composites prepared from eggshell and rice straw&quot;, 《SCIENCE OF THE TOTAL ENVIRONMENT》 (Cat. Y)|吕淑清等: &quot;固体废弃物吸附除磷研究现状&quot;, 《工业水处理》 (Cat. A) CN106902787; CN109012593; US20200023335; CN111135790; CN111253125 LAPSED (CN111672470)|LAPSED DEAD (CN111672470)|DEAD (CN111672470)|LEGAL DETAILS FOR CN111672470|Actual or expected expiration date=2022-11-15|Legal state=DEAD|Status=LAPSED|Event publication date=2020-06-22|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202010572825|Application date=2020-06-22|Standardized application number=2020CN-0572825|Event publication date=2020-09-18|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN111672470|Publication stage code=A|Publication date=2020-09-18|Standardized publication number=CN111672470|Event publication date=2020-09-18|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2020-10-20|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2022-11-15|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQKHUT/vAwmQFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000053915257&ekey=2093&xpn=CN111672470&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=xmTJev82fF5upCKI%252Frgai5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN111672470)|CN (CN111672470)|NAME=TIANJIN UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN111672470)|NAME=WANG XIAN;TIANJIN CAIZHI PATENT&TRADEMARK AGENCY, LTD. , REG=12108 (CN111672470)|NAME=LI GUIJU|NAME=CHEN WENTAO 0 1 Titre: (CN111672470)|Preparation method of charcoal for phosphorus removal Résumé: (CN111672470)|The invention discloses a preparation method of charcoal for phosphorus removal. The preparation method mainly comprises the following steps: mixing dried and crushed sludge with eggshell powder, andcarrying out anaerobic pyrolysis treatment. The invention also discloses a use method of the biological carbon for phosphorus removal. According to the preparation method of the charcoal for phosphorus removal, provided by the invention, municipal residual sludge and waste eggshells are mixed and pyrolyzed to prepare the charcoal, so that resource utilization of wastes is realized, and the problems of relatively low sludge recycling rate, large sludge volume and environmental pollution caused by spoilage at present can be solved to a great extent. The raw materials are rich in source, easy toobtain and low in cost, the method is simple and feasible, and the prepared charcoal has a remarkable and stable removal effect on phosphorus in sewage and wastewater. 118 Abstract gpt-4o-mini no The article focuses on a method for phosphorus removal using charcoal and does not mention CO₂ capture, mineral weathering, or related processes.
120 CN202410545871 CN202410545871 CN118439627 110930449 CN118439627 A 2024-08-06 [CN118439627] 2024-05-06 2024-05-06 2024-08-06 (CN118439627)|2044-05-06 (CN118439627)|Spherical molecular sieve preparation method based on multi-element solid waste sheet layer stacking, corresponding material and application (CN118439627)|The invention relates to the technical field of CO2 adsorption materials, and relates to a preparation method of a multi-solid waste-based lamellar stacked spherical molecular sieve and a corresponding material and application, and the preparation method comprises the following steps: carrying out ball milling and crushing on coal gangue to obtain coal gangue powder, and carrying out carbon removal and activation treatment on the coal gangue powder to obtain carbon-free coal gangue powder; the preparation method comprises the following steps: mixing carbon-free coal gangue powder with sodium hydroxide powder according to a ratio to obtain first mixed powder, and carrying out alkali fusion activation treatment on the first mixed powder to obtain activated carbon-free coal gangue powder; the activated carbon-free coal gangue powder and aluminum ash powder are mixed according to the proportion, second mixed powder is obtained, the second mixed powder is aged with deionized water according to the proportion, and an aged material is obtained; and performing crystallization treatment on the aged material to obtain a crystallized material, and washing and drying the crystallized material to obtain the lamellar stacked spherical molecular sieve. The molecular sieve material for adsorbing CO2 under normal temperature and pressure conditions can be prepared, the CO2 adsorption capacity is remarkably improved, the operation is simple, the repeatability is good, and the cost is low. ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY (CN118439627)|ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN]) WANG QINGPING|XU WEI|MIN JING|CAI JINGYI|YU QINGBO|WEI YONGCHENG|YUAN YUMENG (CN118439627)|WANG QINGPING|XU WEI|MIN JING|CAI JINGYI|YU QINGBO|WEI YONGCHENG|YUAN YUMENG (CN118439627)|WANG HAIRONG;BEIJING SHANGYUE IP AGENCY (GENERAL PARTNERSHIP)|Reg. Nb: 11723 (CN118439627)|The preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve has the advantages of simplicity in operation, good repeatability and low cost, and is suitable for industrial popularization and application.|How to improve the utilization value of the coal gangue is a problem to be solved in the current research.|However, other recycling methods except for extracting and recycling metal aluminum are not mature and complex, and most of the secondary aluminum ash is still in the laboratory research and development stage and is difficult to be used for enterprise production.|Therefore, how to reasonably recycle the solid wastes, reduce the accumulation amount and treat the wastes with the wastes to treat the pollution is one of the key problems of the current research.| (CN118439627)|1. The preparation method of the stacked spherical molecular sieve based on the multiple solid waste sheets is characterized by comprising the following steps: Step one, preparation of carbonless gangue powder Ball milling and crushing the coal gangue to obtain coal gangue powder, and performing carbon removal activation treatment on the coal gangue powder to obtain carbon-free coal gangue powder; Step two, preparation of activated carbon-free gangue powder Mixing the carbon-free coal gangue powder with sodium hydroxide powder according to a proportion to obtain first mixed powder, and performing alkali fusion activation treatment on the first mixed powder to obtain activated carbon-free coal gangue powder; Step three, preparing the lamellar stacked spherical molecular sieve Mixing activated carbon-free coal gangue powder and aluminum ash powder according to a proportion to obtain second mixed powder, and ageing the second mixed powder by adopting deionized water according to the proportion to obtain an ageing material; And (3) crystallizing the aged material to obtain a crystallized material, and washing and drying to obtain the lamellar stacked spherical molecular sieve. | (CN118439627)|According to one aspect of the invention, a preparation method of a stacked spherical molecular sieve based on a plurality of solid waste sheets is provided, and the method comprises the following steps:|The invention relates to the technical field of CO 2 adsorption materials, and relates to a preparation method of a multi-element solid waste sheet stacked spherical molecular sieve, a corresponding material and application, wherein the preparation method comprises the following steps: ball milling and crushing the coal gangue to obtain coal gangue powder, and performing carbon removal activation treatment on the coal gangue powder to obtain carbon-free coal gangue powder; mixing the carbon-free coal gangue powder with sodium hydroxide powder according to a proportion to obtain first mixed powder, and performing alkali fusion activation treatment on the first mixed powder to obtain activated carbon-free coal gangue powder; mixing activated carbon-free coal gangue powder and aluminum ash powder according to a proportion to obtain second mixed powder, and ageing the second mixed powder by adopting deionized water according to the proportion to obtain an ageing material; and (3) crystallizing the aged material to obtain a crystallized material, and washing and drying to obtain the lamellar stacked spherical molecular sieve.|The invention relates to the technical field of CO 2 adsorption materials, in particular to a preparation method of a multi-element solid waste sheet stacked spherical molecular sieve, a corresponding material and application.| (CN118439627)|MOLECULAR SIEVE(100,46)|SOLID WASTE(100,38)|COAL GANGUE POWDER(100,21)|STACKED SPHERICAL MOLECULAR SIEVE(100,21)|SOLID WASTE SHEET(100,12)|COAL GANGUE(75,38)|MIXED POWDER(44,39)|SPHERICAL MOLECULAR SIEVE(42,59)|ALKALI FUSION ACTIVATION TREATMENT(35,10)|FUSION ACTIVATION TREATMENT(33,10)|REPEAT ABILITY(31,3)|POPULARIZATION(31,2)|GANGUE POWDER(29,10)|ALUMINUM ASH(28,17)|MULTIELEMENT SOLID WASTE(24,18)|CARBON REMOVAL ACTIVATION TREATMENT(24,4)|DEIONIZED WATER ADOPTION(24,3)|ALUMINUM ASH POWDER GRANULARITY(23,2)|ENTERPRISE PRODUCTION(21,1)|STACKED SPHERE MOLECULAR SIEVE(21,1)|AGEING MIXED POWDER(19,1)|GANGUE(18,12)|RECYCLING(18,1)|CARBON FREE COAL GANGUE(17,7)|MULTICOMPONENT SOLID WASTE(17,2)|CONTAMINATION(16,1)|NONCARBON GANGUE MASS RATIO(16,1)|MATERIAL CRYSTAL(15,3)|SODIUM HYDROXIDE(14,11)|AGED(14,10)|BALL MILLING(13,14)|ADSORPTION CAPACITY(13,10)|ADSORPTION MATERIAL(13,3)|EXTRACTING(13,1)|AGEING MATERIAL(12,7)|SODIUM HYDROXIDE POWDER(12,4)|LABORATORY RESEARCH(12,1)|REACTION KETTLE(11,6)|STACKED PLATELET TEM MORPHOLOGY(11,2)|LAMELLAR STACKING MORPHOLOGY(10,2)|HEAT PRESERVATION(9,10)|PRODUCT CRYSTAL(9,6)|HEATING RATE(8,4)|ALUMINUM METAL(8,2)|MICROSCOPIC MORPHOLOGY OBSERVATION(8,2)|NONCARBON COAL GANGUE(8,1)|STACKED PELLET MORPHOLOGY REGULARITY(8,1)|DEVELOPMENT STAGE(7,1)|UNTREATED COAL GANGUE(7,1)|STANDING(6,6)|ADOPTING ALKALI FUSION(6,2)|AGED MATERIAL(6,1)|CRUSHING COAL GANGUE(6,1)|RESOURCE UTILIZATION EXPLORATION(6,1)|STACKED PLATELET MORPHOLOGY(6,1)|ADSORBENT MATERIAL(5,2)|SHEET STACKED SPHERE(5,2)|INDUSTRIALIZATION PROGRESS(5,1)|MAGNIFICATION CHARACTERIZATION(5,1)|MOLECULAR SIEVE MATERIAL(5,1)|QUANTACHROME AUTOSORB IQ(5,1)|LAMELLAR STACKING SPHERICAL SHAPE(4,2)|MOLECULAR SIEVE MORPHOLOGY(4,2)|PELLET STACK(4,2)|REGULAR MORPHOLOGY(4,2)|MULTISOLID WASTE SHEET(4,1)|PLATELET SEM MORPHOLOGY DIAGRAM(4,1)|POROSITY ANALYZER(4,1)|STACKING NANOSHEET(4,1)|ROOM TEMPERATURE(3,12)|ACTIVATED CARBON FREE GANGUE(3,10)|CONSTANT TEMPERATURE(3,6)|AGING TREATMENT(3,2)|CRYSTALIZATION TREATMENT(3,2)|HARMFUL SUBSTANCE(3,1)|MULTI COMPONENT SOLID WASTE(3,1)|PEAK INTENSITY(3,1)|PREPARED GANGUE MOLECULAR SIEVE(3,1)| (CN118439627)|1. The preparation method of the stacked spherical molecular sieve based on the multiple solid waste sheets is characterized by comprising the following steps:| Step one, preparation of carbonless gangue powder |Ball milling and crushing the coal gangue to obtain coal gangue powder, and performing carbon removal activation treatment on the coal gangue powder to obtain carbon-free coal gangue powder;| Step two, preparation of activated carbon-free gangue powder |Mixing the carbon-free coal gangue powder with sodium hydroxide powder according to a proportion to obtain first mixed powder, and performing alkali fusion activation treatment on the first mixed powder to obtain activated carbon-free coal gangue powder;| Step three, preparing the lamellar stacked spherical molecular sieve |Mixing activated carbon-free coal gangue powder and aluminum ash powder according to a proportion to obtain second mixed powder, and ageing the second mixed powder by adopting deionized water according to the proportion to obtain an ageing material;| And (3) crystallizing the aged material to obtain a crystallized material, and washing and drying to obtain the lamellar stacked spherical molecular sieve. |2. The method for preparing the stacked spherical molecular sieve based on the multiple solid waste sheets, as claimed in claim 1, is characterized in that in the first step, the gangue is crushed by ball milling to obtain gangue powder, and the method comprises the following steps: crushing the coal gangue into coal gangue powder with the particle size of not more than 75 mu m.|3. The method for preparing the stacked spherical molecular sieve based on the multiple solid waste sheets, which is disclosed in claim 1, is characterized in that in the first step, the carbon removal activation treatment is carried out on the gangue powder, and the method comprises the following steps: heating the gangue powder to 900 ℃ at a heating rate of 10 ℃/min, preserving heat for 3 hours and cooling to room temperature.|4. The preparation method of the stacked spherical molecular sieve based on the multiple solid waste sheets, which is disclosed in claim 1, is characterized in that in the second step, the mass ratio of the non-carbon gangue powder to the sodium hydroxide powder is 1:2, and the granularity of the sodium hydroxide powder is not more than 75 μm.|5. The method for preparing the stacked spherical molecular sieve based on the multiple solid waste sheets according to claim 1, wherein in the second step, alkali fusion activation treatment is performed on the first mixed powder, and the method comprises the following steps: the first mixed powder was heated to 500 c at a heating rate of 10 c/min, incubated for 3h and cooled to room temperature.|6. The preparation method of the stacked spherical molecular sieve based on the multiple solid waste sheets, which is disclosed in claim 1, is characterized in that in the third step, the mass ratio of activated carbon-free gangue powder to aluminum ash powder is 1:0.25-1, and the granularity of the aluminum ash powder is not more than 75 μm.|7. The method for preparing the stacked spherical molecular sieve based on the multiple solid waste sheets, as claimed in claim 1, is characterized in that in the third step, deionized water is used for ageing the second mixed powder according to the proportion, and the method comprises the following steps: and adding the second mixed powder into deionized water according to a proportion, and magnetically stirring and aging for 4 hours under the condition of heating in a water bath at 30 ℃, wherein the mass ratio of the second mixed powder to the deionized water is 1:4.72-5.43.|8. The method for preparing the stacked spherical molecular sieve based on the multiple solid waste sheets, as claimed in claim 1, wherein in the third step, the aged material is crystallized to obtain crystallized material, and the stacked spherical molecular sieve based on the sheets is obtained after washing and drying, and the method comprises the following steps: placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 4-5h at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material with deionized water, and drying at a constant temperature of 60 ℃ for 6h.|9. A multi-component solid waste sheet-based stacked spherical molecular sieve, characterized in that the multi-component solid waste sheet-based stacked spherical molecular sieve is prepared according to the method of any one of claims 1-8.|10. The use of a multi-component solid waste sheet stacked sphere-type molecular sieve based on claim 9 as a CO 2 adsorbent material. (CN118439627)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of CO 2 adsorption materials, in particular to a preparation method of a multi-element solid waste sheet stacked spherical molecular sieve, a corresponding material and application.|BACKGROUND ART|[0002] Gangue and aluminum ash are representative solid wastes. The coal gangue is solid waste generated in the coal mining process, and a large amount of untreated coal gangue is piled up on the ground to occupy the land and pollute the land and a water source; the aluminum ash is solid waste generated in the aluminum smelting process, contains a large amount of alumina, aluminum fluoride and other harmful substances, is randomly stacked or discharged into the environment, and can also cause pollution of soil and water. Therefore, how to reasonably recycle the solid wastes, reduce the accumulation amount and treat the wastes with the wastes to treat the pollution is one of the key problems of the current research. At present, the coal gangue is mainly used for building materials and agriculture, and is used for the most part of the coal gangue to be consumed and utilized. Taking 2022 data as an example, only 3% are used for high value utilization. How to improve the utilization value of the coal gangue is a problem to be solved in the current research. At present, the recycling of primary aluminum ash is mainly performed by recycling metal aluminum, the types of the utilization methods are few, and the types of secondary aluminum ash are more. However, other recycling methods except for extracting and recycling metal aluminum are not mature and complex, and most of the secondary aluminum ash is still in the laboratory research and development stage and is difficult to be used for enterprise production. Therefore, resource utilization exploration of aluminum ash still needs to be studied intensively.|[0003] With the acceleration of the progress of industrialization and the increase of energy consumption, a large amount of CO 2 is released into the atmosphere, resulting in an increase in the concentration of greenhouse gases, which in turn causes serious problems such as extreme weather events, rise in sea level, etc. Therefore, developing efficient CO 2 adsorption technology is of great importance for slowing down climate change, achieving carbon neutralization. At present, related researches on preparing molecular sieves from coal gangue are carried out for CO 2 adsorption, and laboratory researches on how much CO 2 is adsorbed to control the temperature and pressure of the molecular sieves, and the molecular sieves are carried out at high temperature or high pressure, so that energy consumption and cost are increased. The maximum adsorption capacity of the prepared gangue-based molecular sieve at normal temperature and normal pressure is usually not more than 2.5mmol/g. At present, the CO 2 adsorption performance of the gangue-based molecular sieve is improved by carrying out surface modification on the gangue-based molecular sieve, the operation is complex, and the cost is high.|[0004] Therefore, how to provide a method for preparing a CO 2 adsorption material based on multiple solid wastes, which can reduce the preparation cost and the operation complexity, and prepare an adsorption material with excellent CO 2 adsorption capacity at the same time, is a technical problem to be solved.|DISCLOSURE|Disclosure of Invention|[0005] In view of the above, in order to overcome the defects of the prior art, the invention provides a preparation method of a stacked spherical molecular sieve based on a multi-element solid waste sheet, and corresponding materials and applications.|[0006] According to one aspect of the invention, a preparation method of a stacked spherical molecular sieve based on a plurality of solid waste sheets is provided, and the method comprises the following steps:|[0007] Step one, preparation of carbonless gangue powder |[0008] Ball milling and crushing the coal gangue to obtain coal gangue powder, and performing carbon removal activation treatment on the coal gangue powder to obtain carbon-free coal gangue powder;|[0009] Step two, preparation of activated carbon-free gangue powder |[0010] Mixing the carbon-free coal gangue powder with sodium hydroxide powder according to a proportion to obtain first mixed powder, and performing alkali fusion activation treatment on the first mixed powder to obtain activated carbon-free coal gangue powder;|[0011] Step three, preparing the lamellar stacked spherical molecular sieve |[0012] Mixing activated carbon-free coal gangue powder and aluminum ash powder according to a proportion to obtain second mixed powder, and ageing the second mixed powder by adopting deionized water according to the proportion to obtain an ageing material;|[0013] And (3) crystallizing the aged material to obtain a crystallized material, and washing and drying to obtain the lamellar stacked spherical molecular sieve. |[0014] Preferably, the preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve comprises the following steps of ball milling and crushing coal gangue to obtain coal gangue powder: crushing the coal gangue into coal gangue powder with the particle size of not more than 75 mu m.|[0015] Preferably, the preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve comprises the following steps of: heating the gangue powder to 900 ℃ at a heating rate of 10 ℃/min, preserving heat for 3 hours and cooling to room temperature.|[0016] Preferably, the preparation method is based on a multi-element solid waste sheet stacked spherical molecular sieve, in the second step, the mass ratio of the non-carbon coal gangue powder to the sodium hydroxide powder is 1:2, and the granularity of the sodium hydroxide powder is not more than 75 mu m.|[0017] Preferably, the preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve comprises the following steps of: the first mixed powder was heated to 500 c at a heating rate of 10 c/min, incubated for 3h and cooled to room temperature.|[0018] Preferably, the preparation method is based on a multi-element solid waste sheet stacked spherical molecular sieve, and in the third step, the mass ratio of activated carbon-free gangue powder to aluminum ash powder is 1:0.25-1, and the granularity of the aluminum ash powder is not more than 75 mu m.|[0019] Preferably, the preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve comprises the following steps: and adding the second mixed powder into deionized water according to a proportion, and magnetically stirring and aging for 4 hours under the condition of heating in a water bath at 30 ℃, wherein the mass ratio of the second mixed powder to the deionized water is 1:4.72-5.43.|[0020] Preferably, the preparation method based on the multi-element solid waste lamellar stacked spherical molecular sieve comprises the following steps of crystallizing the aged material to obtain crystallized material, washing and drying to obtain lamellar stacked spherical molecular sieve, wherein the preparation method comprises the following steps: placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 4-5h at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material with deionized water, and drying at a constant temperature of 60 ℃ for 6h.|[0021] According to another aspect of the present invention, there is provided a multi-solid waste sheet stacked spherical molecular sieve based produced according to the above-described method.|[0022] According to a further aspect, the invention relates to the use of a stacked spherical molecular sieve based on multiple solid waste lamellae as CO 2 adsorbent material.|[0023] The preparation method of the stacked spherical molecular sieve based on the multiple solid waste sheets and the corresponding materials and applications have the following beneficial effects:|[0024] 1. Adopting alkali fusion activated carbon-free gangue powder and aluminum ash to prepare a stacked spherical molecular sieve based on multiple solid waste slices together, wherein the raw materials are solid wastes; activated carbon-free gangue powder is obtained through carbon removal activation and alkali fusion activation treatment, so that the utilization rate of silicon-aluminum components in the gangue is improved while the preparation cost is reduced; |[0025] 2. The molecular sieve morphology is regulated and controlled through aging treatment and crystallization treatment by controlling the mass ratio of activated carbon-free gangue powder to aluminum ash powder, so that the molecular sieve with the lamellar stacking spherical shape, regular morphology and uniform size is synthesized, the specific surface area of the molecular sieve is improved through the lamellar stacking morphology, and the CO 2 adsorption capacity is remarkably improved; |[0026] 3. The spherical molecular sieve based on the multi-element solid waste lamellar stack prepared by the invention can realize the adsorption of CO 2 under the conditions of normal temperature and normal pressure, avoids the energy consumption and the increase of cost caused by high-temperature and high-pressure operation, obviously improves the applicability and the flexibility of material adsorption by CO 2 adsorption under the conditions of normal temperature and normal pressure, and has wide prospect in industrial application; |[0027] 4. The preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve has the advantages of simplicity in operation, good repeatability and low cost, and is suitable for industrial popularization and application. |DRAWINGS DESCRIPTION|[0028] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.|[0029] FIG. 1 is a SEM morphology diagram of 4000 times of a platelet stacked spherical molecular sieve prepared in example 1 of the present invention;|[0030] FIG. 2 is an SEM morphology diagram of a platelet stacked spherical molecular sieve prepared in example 1 of the present invention at 20000 times; |[0031] FIG. 3 is a SEM morphology of 4000 times of the platelet stacked spherical molecular sieve prepared in example 3 of the present invention; |[0032] FIG. 4 is an SEM morphology diagram of a stacked platelet spherical molecular sieve prepared in example 3 of the present invention at 20000 times; |[0033] FIG. 5 is a SEM morphology of 4000 times of the platelet stacked spherical molecular sieve prepared in example 4 of the present invention; |[0034] FIG. 6 is an SEM morphology of a stacked platelet morphology of a spherical molecular sieve at 20000 times; |[0035] FIG. 7 is a TEM morphology of the stacked platelet spherical molecular sieve prepared in example 4 of the present invention at 20000 times; |[0036] FIG. 8 is a TEM morphology of the stacked platelet spherical molecular sieve of example 4 of the present invention at 50000 times; |[0037] FIG. 9 is a test result of the crystal structure of the platelet stacked spherical molecular sieve prepared in example 1 of the present invention; |[0038] FIG. 10 is a test result of the crystal structure of the platelet stacked spherical molecular sieve prepared in example 2 of the present invention; |[0039] FIG. 11 is a test result of the crystal structure of the platelet stacked spherical molecular sieve prepared in example 3 of the present invention; |[0040] fig. 12 is a crystal structure test result of the platelet stacked spherical molecular sieve prepared in example 4 of the present invention. |INVENTION MODE|Detailed Description|[0041] Embodiments of the present invention will be described in detail below with reference to the accompanying drawings.|[0042] It should be noted that, without conflict, the following embodiments and features in the embodiments may be combined with each other; and, based on the embodiments in this disclosure, all other embodiments that may be made by one of ordinary skill in the art without inventive effort are within the scope of the present disclosure.|[0043] It is noted that various aspects of the embodiments are described below within the scope of the following claims. It should be apparent that the aspects described herein may be embodied in a wide variety of forms and that any specific structure and/or function described herein is merely illustrative. Based on the present disclosure, one skilled in the art will appreciate that one aspect described herein may be implemented independently of any other aspect, and that two or more of these aspects may be combined in various ways. For example, an apparatus may be implemented and/or a method practiced using any number of the aspects set forth herein. In addition, such apparatus may be implemented and/or such methods practiced using other structure and/or functionality in addition to one or more of the aspects set forth herein.|[0044] Example 1|[0045] Preparation of a stacked spherical molecular sieve based on a multi-element solid waste sheet:|[0046] Step one, preparation of carbonless gangue powder |[0047] Ball milling and crushing the coal gangue, ball milling and crushing the coal gangue to coal gangue powder with the particle size of not more than 75 mu m, heating the coal gangue powder to 900 ℃ at the heating rate of 10 ℃/min, preserving heat for 3 hours, and cooling to room temperature to obtain carbon-free coal gangue powder;|[0048] Step two, preparation of activated carbon-free gangue powder |[0049] Mixing the carbon-free coal gangue powder with sodium hydroxide powder with the granularity not more than 75 mu m according to the mass ratio of 1:2 to obtain first mixed powder, performing alkali fusion activation treatment on the first mixed powder, heating the first mixed powder to 500 ℃ at the heating rate of 10 ℃/min, preserving heat for 3h, and cooling to room temperature to obtain activated carbon-free coal gangue powder;|[0050] Step three, preparing the lamellar stacked spherical molecular sieve |[0051] Mixing activated carbon-free gangue powder with aluminum ash powder with granularity not more than 75 mu m according to the mass ratio of 1:0.25 to obtain second mixed powder, adding the second mixed powder into deionized water according to the mass ratio of 1:5.43, and magnetically stirring and ageing for 4 hours under the water bath heating condition of 30 ℃ to obtain an ageing material;|[0052] Placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 5 hours at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material by deionized water, and drying at a constant temperature of 60 ℃ for 6 hours to obtain the lamellar stacked spherical molecular sieve. |[0053] Example 2|[0054] Preparation of a stacked spherical molecular sieve based on a multi-element solid waste sheet:|[0055] Step one, preparation of carbonless gangue powder |[0056] Ball milling and crushing the coal gangue, ball milling and crushing the coal gangue to coal gangue powder with the particle size of not more than 75 mu m, heating the coal gangue powder to 900 ℃ at the heating rate of 10 ℃/min, preserving heat for 3 hours, and cooling to room temperature to obtain carbon-free coal gangue powder;|[0057] Step two, preparation of activated carbon-free gangue powder |[0058] Mixing the carbon-free coal gangue powder with sodium hydroxide powder with the granularity not more than 75 mu m according to the mass ratio of 1:2 to obtain first mixed powder, performing alkali fusion activation treatment on the first mixed powder, heating the first mixed powder to 500 ℃ at the heating rate of 10 ℃/min, preserving heat for 3h, and cooling to room temperature to obtain activated carbon-free coal gangue powder;|[0059] Step three, preparing the lamellar stacked spherical molecular sieve |[0060] Mixing activated carbon-free gangue powder and aluminum ash powder with granularity not more than 75 mu m according to the mass ratio of 1:0.5 to obtain second mixed powder, adding the second mixed powder into deionized water according to the mass ratio of 1:5.03, and magnetically stirring and ageing for 4 hours under the water bath heating condition of 30 ℃ to obtain an ageing material;|[0061] placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 4.5 hours at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material by deionized water, and drying at a constant temperature of 60 ℃ for 6 hours to obtain the lamellar stacked spherical molecular sieve. |[0062] Example 3|[0063] Preparation of a stacked spherical molecular sieve based on a multi-element solid waste sheet:|[0064] Step one, preparation of carbonless gangue powder |[0065] Ball milling and crushing the coal gangue, ball milling and crushing the coal gangue to coal gangue powder with the particle size of not more than 75 mu m, heating the coal gangue powder to 900 ℃ at the heating rate of 10 ℃/min, preserving heat for 3 hours, and cooling to room temperature to obtain carbon-free coal gangue powder;|[0066] Step two, preparation of activated carbon-free gangue powder |[0067] Mixing the carbon-free coal gangue powder with sodium hydroxide powder with the granularity not more than 75 mu m according to the mass ratio of 1:2 to obtain first mixed powder, performing alkali fusion activation treatment on the first mixed powder, heating the first mixed powder to 500 ℃ at the heating rate of 10 ℃/min, preserving heat for 3h, and cooling to room temperature to obtain activated carbon-free coal gangue powder;|[0068] Step three, preparing the lamellar stacked spherical molecular sieve |[0069] Mixing activated carbon-free gangue powder and aluminum ash powder with granularity not more than 75 mu m according to the mass ratio of 1:1 to obtain second mixed powder, adding the second mixed powder into deionized water according to the mass ratio of 1:4.72, and magnetically stirring and ageing for 4 hours under the water bath heating condition of 30 ℃ to obtain an ageing material;|[0070] Placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 4 hours at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material by deionized water, and drying at a constant temperature of 60 ℃ for 6 hours to obtain the lamellar stacked spherical molecular sieve. |[0071] Example 4|[0072] Preparation of a stacked spherical molecular sieve based on a multi-element solid waste sheet:|[0073] Step one, preparation of carbonless gangue powder |[0074] Ball milling and crushing the coal gangue, ball milling and crushing the coal gangue to coal gangue powder with the particle size of not more than 75 mu m, heating the coal gangue powder to 900 ℃ at the heating rate of 10 ℃/min, preserving heat for 3 hours, and cooling to room temperature to obtain carbon-free coal gangue powder;|[0075] Step two, preparation of activated carbon-free gangue powder |[0076] Mixing the carbon-free coal gangue powder with sodium hydroxide powder with the granularity not more than 75 mu m according to the mass ratio of 1:2 to obtain first mixed powder, performing alkali fusion activation treatment on the first mixed powder, heating the first mixed powder to 500 ℃ at the heating rate of 10 ℃/min, preserving heat for 3h, and cooling to room temperature to obtain activated carbon-free coal gangue powder;|[0077] Step three, preparing the lamellar stacked spherical molecular sieve |[0078] Mixing activated carbon-free gangue powder and aluminum ash powder with granularity not more than 75 mu m according to the mass ratio of 1:0.5 to obtain second mixed powder, adding the second mixed powder into deionized water according to the mass ratio of 1:5.03, and magnetically stirring and ageing for 4 hours under the water bath heating condition of 30 ℃ to obtain an ageing material;|[0079] Placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 5 hours at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material by deionized water, and drying at a constant temperature of 60 ℃ for 6 hours to obtain the lamellar stacked spherical molecular sieve. |[0080] Example 5|[0081] Microscopic morphology observation and characterization of different magnifications are carried out on the lamellar stacked spherical molecular sieves prepared in the examples 1, 3 and 4 by adopting a Hitachi Regulus8100 scanning electron microscope, wherein the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 1 is 4000 times and is shown in fig. 1, the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 1 is 20000 times and is shown in fig. 2, the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 3 is 4000 times and is shown in fig. 3, the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 3 is 20000 times and is shown in fig. 4, the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 4 is 4000 times and is shown in fig. 5, and the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 4 is 20000 times and is shown in fig. 6. The molecular sieve prepared in example 1 has a morphology of stacked spheres of sheets, as shown in fig. 1, and the proportion of stacked spheres of sheets in the molecular sieves prepared in example 3 and example 4 gradually increases as the addition amount of aluminum ash and crystallization time increase, as shown in fig. 3 and 5. Meanwhile, as the addition amount of aluminum ash and crystallization time are increased, as shown in fig. 2, 4 and 6, the morphology size of the obtained molecular sieve is more uniform, and the morphology regularity is gradually improved.|[0082] Microscopic morphology observation and characterization were performed on the platelet-stacked spherical molecular sieve prepared in example 4 by using a transmission electron microscope (FEI Talos F200X G2), the morphology of the platelet-stacked spherical molecular sieve prepared in example 4 is 20000 times TEM, see fig. 7, and the morphology of the platelet-stacked spherical molecular sieve prepared in example 4 is 50000 times TEM, see fig. 8. As shown in fig. 7 and 8, the molecular sieve prepared in example 4 can be seen to be formed into a sphere by stacking nano-sheets, and the stacking of sheets provides a larger specific surface area for the molecular sieve.|[0083] The crystal structures of the sheet stacked spherical molecular sieves prepared in examples 1, 2, 3 and 4 were tested using an X-ray diffractometer (Shimadzu XRD-6000), and the crystal structure test results of the sheet stacked spherical molecular sieves prepared in examples 1 to 4 are shown in fig. 9, 10, 11 and 12, respectively. As shown in fig. 9, a type a molecular sieve characteristic peak has appeared in the sheet stacked spherical molecular sieve prepared in example 1. As shown in fig. 10, 11 and 12, the stacked pellet type molecular sieves prepared in examples 2-4 all belong to a type a molecular sieve, and as the addition amount of aluminum ash and the crystallization time increase, the characteristic peak intensity of the type a molecular sieve gradually increases, which indicates that the crystallinity gradually increases, which corresponds to the increase in the morphology regularity of the stacked pellet type molecular sieves in fig. 2, 4 and 6.|[0084] The sheet stacked spherical molecular sieves prepared in examples 1,2, 3, and 4 were subjected to CO 2 adsorption tests at 101.325kPa and 298.15K using a fully automatic specific surface area and porosity analyzer (Quantachrome Autosorb IQ). The adsorption capacity of the lamellar stacked spherical molecular sieve prepared in example 1 was 2.61mmol/g. The adsorption capacity of the lamellar stacked spherical molecular sieve prepared in example 2 was 2.72mmol/g. The adsorption capacity of the lamellar stacked spherical molecular sieve prepared in example 3 was 2.86mmol/g. The adsorption capacity of the lamellar stacked spherical molecular sieve prepared in example 4 was 2.91mmol/g. The adsorption capacity of CO 2 of the lamellar stacked spherical molecular sieve prepared in the examples 1-4 is more than 2.5mmol/g at normal temperature and normal pressure, and the adsorption effect is good. And as the addition amount of aluminum ash and crystallization time are increased, the adsorption capacity of the lamellar stacked spherical molecular sieve prepared in examples 1-4 is gradually increased, which is attributed to the improvement of the morphology regularity and the crystallinity of the molecular sieve as shown in fig. 2,4, 6 and 9-12.|[0085] The preparation method of the stacked spherical molecular sieve based on the multiple solid waste sheets and the corresponding materials and applications have the following beneficial effects:|[0086] 1. Adopting alkali fusion activated carbon-free gangue powder and aluminum ash to prepare a stacked spherical molecular sieve based on multiple solid waste slices together, wherein the raw materials are solid wastes; activated carbon-free gangue powder is obtained through carbon removal activation and alkali fusion activation treatment, so that the utilization rate of silicon-aluminum components in the gangue is improved while the preparation cost is reduced; |[0087] 2. The molecular sieve morphology is regulated and controlled through aging treatment and crystallization treatment by controlling the mass ratio of activated carbon-free gangue powder to aluminum ash powder, so that the molecular sieve with the lamellar stacking spherical shape, regular morphology and uniform size is synthesized, the specific surface area of the molecular sieve is improved through the lamellar stacking morphology, and the CO 2 adsorption capacity is remarkably improved; |[0088] 3. The spherical molecular sieve based on the multi-element solid waste lamellar stack prepared by the invention can realize the adsorption of CO 2 under the conditions of normal temperature and normal pressure, avoids the energy consumption and the increase of cost caused by high-temperature and high-pressure operation, obviously improves the applicability and the flexibility of material adsorption by CO 2 adsorption under the conditions of normal temperature and normal pressure, and has wide prospect in industrial application; |[0089] 4. The preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve has the advantages of simplicity in operation, good repeatability and low cost, and is suitable for industrial popularization and application. |[0090] The foregoing is merely illustrative of the present invention, and the present invention is not limited thereto, and any changes or substitutions easily contemplated by those skilled in the art within the scope of the present invention should be included in the present invention. Therefore, the protection scope of the invention is subject to the protection scope of the claims. (CN118439627)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of CO 2 adsorption materials, in particular to a preparation method of a multi-element solid waste sheet stacked spherical molecular sieve, a corresponding material and application.|BACKGROUND ART|[0002] Gangue and aluminum ash are representative solid wastes. The coal gangue is solid waste generated in the coal mining process, and a large amount of untreated coal gangue is piled up on the ground to occupy the land and pollute the land and a water source; the aluminum ash is solid waste generated in the aluminum smelting process, contains a large amount of alumina, aluminum fluoride and other harmful substances, is randomly stacked or discharged into the environment, and can also cause pollution of soil and water. Therefore, how to reasonably recycle the solid wastes, reduce the accumulation amount and treat the wastes with the wastes to treat the pollution is one of the key problems of the current research. At present, the coal gangue is mainly used for building materials and agriculture, and is used for the most part of the coal gangue to be consumed and utilized. Taking 2022 data as an example, only 3% are used for high value utilization. How to improve the utilization value of the coal gangue is a problem to be solved in the current research. At present, the recycling of primary aluminum ash is mainly performed by recycling metal aluminum, the types of the utilization methods are few, and the types of secondary aluminum ash are more. However, other recycling methods except for extracting and recycling metal aluminum are not mature and complex, and most of the secondary aluminum ash is still in the laboratory research and development stage and is difficult to be used for enterprise production. Therefore, resource utilization exploration of aluminum ash still needs to be studied intensively.|[0003] With the acceleration of the progress of industrialization and the increase of energy consumption, a large amount of CO 2 is released into the atmosphere, resulting in an increase in the concentration of greenhouse gases, which in turn causes serious problems such as extreme weather events, rise in sea level, etc. Therefore, developing efficient CO 2 adsorption technology is of great importance for slowing down climate change, achieving carbon neutralization. At present, related researches on preparing molecular sieves from coal gangue are carried out for CO 2 adsorption, and laboratory researches on how much CO 2 is adsorbed to control the temperature and pressure of the molecular sieves, and the molecular sieves are carried out at high temperature or high pressure, so that energy consumption and cost are increased. The maximum adsorption capacity of the prepared gangue-based molecular sieve at normal temperature and normal pressure is usually not more than 2.5mmol/g. At present, the CO 2 adsorption performance of the gangue-based molecular sieve is improved by carrying out surface modification on the gangue-based molecular sieve, the operation is complex, and the cost is high.|[0004] Therefore, how to provide a method for preparing a CO 2 adsorption material based on multiple solid wastes, which can reduce the preparation cost and the operation complexity, and prepare an adsorption material with excellent CO 2 adsorption capacity at the same time, is a technical problem to be solved.|DISCLOSURE|Disclosure of Invention|[0005] In view of the above, in order to overcome the defects of the prior art, the invention provides a preparation method of a stacked spherical molecular sieve based on a multi-element solid waste sheet, and corresponding materials and applications.|[0006] According to one aspect of the invention, a preparation method of a stacked spherical molecular sieve based on a plurality of solid waste sheets is provided, and the method comprises the following steps:|[0007] Step one, preparation of carbonless gangue powder |[0008] Ball milling and crushing the coal gangue to obtain coal gangue powder, and performing carbon removal activation treatment on the coal gangue powder to obtain carbon-free coal gangue powder;|[0009] Step two, preparation of activated carbon-free gangue powder |[0010] Mixing the carbon-free coal gangue powder with sodium hydroxide powder according to a proportion to obtain first mixed powder, and performing alkali fusion activation treatment on the first mixed powder to obtain activated carbon-free coal gangue powder;|[0011] Step three, preparing the lamellar stacked spherical molecular sieve |[0012] Mixing activated carbon-free coal gangue powder and aluminum ash powder according to a proportion to obtain second mixed powder, and ageing the second mixed powder by adopting deionized water according to the proportion to obtain an ageing material;|[0013] And (3) crystallizing the aged material to obtain a crystallized material, and washing and drying to obtain the lamellar stacked spherical molecular sieve. |[0014] Preferably, the preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve comprises the following steps of ball milling and crushing coal gangue to obtain coal gangue powder: crushing the coal gangue into coal gangue powder with the particle size of not more than 75 mu m.|[0015] Preferably, the preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve comprises the following steps of: heating the gangue powder to 900 ℃ at a heating rate of 10 ℃/min, preserving heat for 3 hours and cooling to room temperature.|[0016] Preferably, the preparation method is based on a multi-element solid waste sheet stacked spherical molecular sieve, in the second step, the mass ratio of the non-carbon coal gangue powder to the sodium hydroxide powder is 1:2, and the granularity of the sodium hydroxide powder is not more than 75 mu m.|[0017] Preferably, the preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve comprises the following steps of: the first mixed powder was heated to 500 c at a heating rate of 10 c/min, incubated for 3h and cooled to room temperature.|[0018] Preferably, the preparation method is based on a multi-element solid waste sheet stacked spherical molecular sieve, and in the third step, the mass ratio of activated carbon-free gangue powder to aluminum ash powder is 1:0.25-1, and the granularity of the aluminum ash powder is not more than 75 mu m.|[0019] Preferably, the preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve comprises the following steps: and adding the second mixed powder into deionized water according to a proportion, and magnetically stirring and aging for 4 hours under the condition of heating in a water bath at 30 ℃, wherein the mass ratio of the second mixed powder to the deionized water is 1:4.72-5.43.|[0020] Preferably, the preparation method based on the multi-element solid waste lamellar stacked spherical molecular sieve comprises the following steps of crystallizing the aged material to obtain crystallized material, washing and drying to obtain lamellar stacked spherical molecular sieve, wherein the preparation method comprises the following steps: placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 4-5h at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material with deionized water, and drying at a constant temperature of 60 ℃ for 6h.|[0021] According to another aspect of the present invention, there is provided a multi-solid waste sheet stacked spherical molecular sieve based produced according to the above-described method.|[0022] According to a further aspect, the invention relates to the use of a stacked spherical molecular sieve based on multiple solid waste lamellae as CO 2 adsorbent material.|[0023] The preparation method of the stacked spherical molecular sieve based on the multiple solid waste sheets and the corresponding materials and applications have the following beneficial effects:|[0024] 1. Adopting alkali fusion activated carbon-free gangue powder and aluminum ash to prepare a stacked spherical molecular sieve based on multiple solid waste slices together, wherein the raw materials are solid wastes; activated carbon-free gangue powder is obtained through carbon removal activation and alkali fusion activation treatment, so that the utilization rate of silicon-aluminum components in the gangue is improved while the preparation cost is reduced; |[0025] 2. The molecular sieve morphology is regulated and controlled through aging treatment and crystallization treatment by controlling the mass ratio of activated carbon-free gangue powder to aluminum ash powder, so that the molecular sieve with the lamellar stacking spherical shape, regular morphology and uniform size is synthesized, the specific surface area of the molecular sieve is improved through the lamellar stacking morphology, and the CO 2 adsorption capacity is remarkably improved; |[0026] 3. The spherical molecular sieve based on the multi-element solid waste lamellar stack prepared by the invention can realize the adsorption of CO 2 under the conditions of normal temperature and normal pressure, avoids the energy consumption and the increase of cost caused by high-temperature and high-pressure operation, obviously improves the applicability and the flexibility of material adsorption by CO 2 adsorption under the conditions of normal temperature and normal pressure, and has wide prospect in industrial application; |[0027] 4. The preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve has the advantages of simplicity in operation, good repeatability and low cost, and is suitable for industrial popularization and application. |DRAWINGS DESCRIPTION|[0028] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.|[0029] FIG. 1 is a SEM morphology diagram of 4000 times of a platelet stacked spherical molecular sieve prepared in example 1 of the present invention;|[0030] FIG. 2 is an SEM morphology diagram of a platelet stacked spherical molecular sieve prepared in example 1 of the present invention at 20000 times; |[0031] FIG. 3 is a SEM morphology of 4000 times of the platelet stacked spherical molecular sieve prepared in example 3 of the present invention; |[0032] FIG. 4 is an SEM morphology diagram of a stacked platelet spherical molecular sieve prepared in example 3 of the present invention at 20000 times; |[0033] FIG. 5 is a SEM morphology of 4000 times of the platelet stacked spherical molecular sieve prepared in example 4 of the present invention; |[0034] FIG. 6 is an SEM morphology of a stacked platelet morphology of a spherical molecular sieve at 20000 times; |[0035] FIG. 7 is a TEM morphology of the stacked platelet spherical molecular sieve prepared in example 4 of the present invention at 20000 times; |[0036] FIG. 8 is a TEM morphology of the stacked platelet spherical molecular sieve of example 4 of the present invention at 50000 times; |[0037] FIG. 9 is a test result of the crystal structure of the platelet stacked spherical molecular sieve prepared in example 1 of the present invention; |[0038] FIG. 10 is a test result of the crystal structure of the platelet stacked spherical molecular sieve prepared in example 2 of the present invention; |[0039] FIG. 11 is a test result of the crystal structure of the platelet stacked spherical molecular sieve prepared in example 3 of the present invention; |[0040] fig. 12 is a crystal structure test result of the platelet stacked spherical molecular sieve prepared in example 4 of the present invention. |INVENTION MODE|Detailed Description|[0041] Embodiments of the present invention will be described in detail below with reference to the accompanying drawings.|[0042] It should be noted that, without conflict, the following embodiments and features in the embodiments may be combined with each other; and, based on the embodiments in this disclosure, all other embodiments that may be made by one of ordinary skill in the art without inventive effort are within the scope of the present disclosure.|[0043] It is noted that various aspects of the embodiments are described below within the scope of the following claims. It should be apparent that the aspects described herein may be embodied in a wide variety of forms and that any specific structure and/or function described herein is merely illustrative. Based on the present disclosure, one skilled in the art will appreciate that one aspect described herein may be implemented independently of any other aspect, and that two or more of these aspects may be combined in various ways. For example, an apparatus may be implemented and/or a method practiced using any number of the aspects set forth herein. In addition, such apparatus may be implemented and/or such methods practiced using other structure and/or functionality in addition to one or more of the aspects set forth herein.|[0044] Example 1|[0045] Preparation of a stacked spherical molecular sieve based on a multi-element solid waste sheet:|[0046] Step one, preparation of carbonless gangue powder |[0047] Ball milling and crushing the coal gangue, ball milling and crushing the coal gangue to coal gangue powder with the particle size of not more than 75 mu m, heating the coal gangue powder to 900 ℃ at the heating rate of 10 ℃/min, preserving heat for 3 hours, and cooling to room temperature to obtain carbon-free coal gangue powder;|[0048] Step two, preparation of activated carbon-free gangue powder |[0049] Mixing the carbon-free coal gangue powder with sodium hydroxide powder with the granularity not more than 75 mu m according to the mass ratio of 1:2 to obtain first mixed powder, performing alkali fusion activation treatment on the first mixed powder, heating the first mixed powder to 500 ℃ at the heating rate of 10 ℃/min, preserving heat for 3h, and cooling to room temperature to obtain activated carbon-free coal gangue powder;|[0050] Step three, preparing the lamellar stacked spherical molecular sieve |[0051] Mixing activated carbon-free gangue powder with aluminum ash powder with granularity not more than 75 mu m according to the mass ratio of 1:0.25 to obtain second mixed powder, adding the second mixed powder into deionized water according to the mass ratio of 1:5.43, and magnetically stirring and ageing for 4 hours under the water bath heating condition of 30 ℃ to obtain an ageing material;|[0052] Placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 5 hours at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material by deionized water, and drying at a constant temperature of 60 ℃ for 6 hours to obtain the lamellar stacked spherical molecular sieve. |[0053] Example 2|[0054] Preparation of a stacked spherical molecular sieve based on a multi-element solid waste sheet:|[0055] Step one, preparation of carbonless gangue powder |[0056] Ball milling and crushing the coal gangue, ball milling and crushing the coal gangue to coal gangue powder with the particle size of not more than 75 mu m, heating the coal gangue powder to 900 ℃ at the heating rate of 10 ℃/min, preserving heat for 3 hours, and cooling to room temperature to obtain carbon-free coal gangue powder;|[0057] Step two, preparation of activated carbon-free gangue powder |[0058] Mixing the carbon-free coal gangue powder with sodium hydroxide powder with the granularity not more than 75 mu m according to the mass ratio of 1:2 to obtain first mixed powder, performing alkali fusion activation treatment on the first mixed powder, heating the first mixed powder to 500 ℃ at the heating rate of 10 ℃/min, preserving heat for 3h, and cooling to room temperature to obtain activated carbon-free coal gangue powder;|[0059] Step three, preparing the lamellar stacked spherical molecular sieve |[0060] Mixing activated carbon-free gangue powder and aluminum ash powder with granularity not more than 75 mu m according to the mass ratio of 1:0.5 to obtain second mixed powder, adding the second mixed powder into deionized water according to the mass ratio of 1:5.03, and magnetically stirring and ageing for 4 hours under the water bath heating condition of 30 ℃ to obtain an ageing material;|[0061] placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 4.5 hours at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material by deionized water, and drying at a constant temperature of 60 ℃ for 6 hours to obtain the lamellar stacked spherical molecular sieve. |[0062] Example 3|[0063] Preparation of a stacked spherical molecular sieve based on a multi-element solid waste sheet:|[0064] Step one, preparation of carbonless gangue powder |[0065] Ball milling and crushing the coal gangue, ball milling and crushing the coal gangue to coal gangue powder with the particle size of not more than 75 mu m, heating the coal gangue powder to 900 ℃ at the heating rate of 10 ℃/min, preserving heat for 3 hours, and cooling to room temperature to obtain carbon-free coal gangue powder;|[0066] Step two, preparation of activated carbon-free gangue powder |[0067] Mixing the carbon-free coal gangue powder with sodium hydroxide powder with the granularity not more than 75 mu m according to the mass ratio of 1:2 to obtain first mixed powder, performing alkali fusion activation treatment on the first mixed powder, heating the first mixed powder to 500 ℃ at the heating rate of 10 ℃/min, preserving heat for 3h, and cooling to room temperature to obtain activated carbon-free coal gangue powder;|[0068] Step three, preparing the lamellar stacked spherical molecular sieve |[0069] Mixing activated carbon-free gangue powder and aluminum ash powder with granularity not more than 75 mu m according to the mass ratio of 1:1 to obtain second mixed powder, adding the second mixed powder into deionized water according to the mass ratio of 1:4.72, and magnetically stirring and ageing for 4 hours under the water bath heating condition of 30 ℃ to obtain an ageing material;|[0070] Placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 4 hours at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material by deionized water, and drying at a constant temperature of 60 ℃ for 6 hours to obtain the lamellar stacked spherical molecular sieve. |[0071] Example 4|[0072] Preparation of a stacked spherical molecular sieve based on a multi-element solid waste sheet:|[0073] Step one, preparation of carbonless gangue powder |[0074] Ball milling and crushing the coal gangue, ball milling and crushing the coal gangue to coal gangue powder with the particle size of not more than 75 mu m, heating the coal gangue powder to 900 ℃ at the heating rate of 10 ℃/min, preserving heat for 3 hours, and cooling to room temperature to obtain carbon-free coal gangue powder;|[0075] Step two, preparation of activated carbon-free gangue powder |[0076] Mixing the carbon-free coal gangue powder with sodium hydroxide powder with the granularity not more than 75 mu m according to the mass ratio of 1:2 to obtain first mixed powder, performing alkali fusion activation treatment on the first mixed powder, heating the first mixed powder to 500 ℃ at the heating rate of 10 ℃/min, preserving heat for 3h, and cooling to room temperature to obtain activated carbon-free coal gangue powder;|[0077] Step three, preparing the lamellar stacked spherical molecular sieve |[0078] Mixing activated carbon-free gangue powder and aluminum ash powder with granularity not more than 75 mu m according to the mass ratio of 1:0.5 to obtain second mixed powder, adding the second mixed powder into deionized water according to the mass ratio of 1:5.03, and magnetically stirring and ageing for 4 hours under the water bath heating condition of 30 ℃ to obtain an ageing material;|[0079] Placing the aged material into a high-pressure reaction kettle, standing and crystallizing for 5 hours at 110 ℃, filtering the crystallized product to obtain a solid material, washing the solid material by deionized water, and drying at a constant temperature of 60 ℃ for 6 hours to obtain the lamellar stacked spherical molecular sieve. |[0080] Example 5|[0081] Microscopic morphology observation and characterization of different magnifications are carried out on the lamellar stacked spherical molecular sieves prepared in the examples 1, 3 and 4 by adopting a Hitachi Regulus8100 scanning electron microscope, wherein the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 1 is 4000 times and is shown in fig. 1, the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 1 is 20000 times and is shown in fig. 2, the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 3 is 4000 times and is shown in fig. 3, the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 3 is 20000 times and is shown in fig. 4, the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 4 is 4000 times and is shown in fig. 5, and the SEM morphology of the lamellar stacked spherical molecular sieve prepared in the example 4 is 20000 times and is shown in fig. 6. The molecular sieve prepared in example 1 has a morphology of stacked spheres of sheets, as shown in fig. 1, and the proportion of stacked spheres of sheets in the molecular sieves prepared in example 3 and example 4 gradually increases as the addition amount of aluminum ash and crystallization time increase, as shown in fig. 3 and 5. Meanwhile, as the addition amount of aluminum ash and crystallization time are increased, as shown in fig. 2, 4 and 6, the morphology size of the obtained molecular sieve is more uniform, and the morphology regularity is gradually improved.|[0082] Microscopic morphology observation and characterization were performed on the platelet-stacked spherical molecular sieve prepared in example 4 by using a transmission electron microscope (FEI Talos F200X G2), the morphology of the platelet-stacked spherical molecular sieve prepared in example 4 is 20000 times TEM, see fig. 7, and the morphology of the platelet-stacked spherical molecular sieve prepared in example 4 is 50000 times TEM, see fig. 8. As shown in fig. 7 and 8, the molecular sieve prepared in example 4 can be seen to be formed into a sphere by stacking nano-sheets, and the stacking of sheets provides a larger specific surface area for the molecular sieve.|[0083] The crystal structures of the sheet stacked spherical molecular sieves prepared in examples 1, 2, 3 and 4 were tested using an X-ray diffractometer (Shimadzu XRD-6000), and the crystal structure test results of the sheet stacked spherical molecular sieves prepared in examples 1 to 4 are shown in fig. 9, 10, 11 and 12, respectively. As shown in fig. 9, a type a molecular sieve characteristic peak has appeared in the sheet stacked spherical molecular sieve prepared in example 1. As shown in fig. 10, 11 and 12, the stacked pellet type molecular sieves prepared in examples 2-4 all belong to a type a molecular sieve, and as the addition amount of aluminum ash and the crystallization time increase, the characteristic peak intensity of the type a molecular sieve gradually increases, which indicates that the crystallinity gradually increases, which corresponds to the increase in the morphology regularity of the stacked pellet type molecular sieves in fig. 2, 4 and 6.|[0084] The sheet stacked spherical molecular sieves prepared in examples 1,2, 3, and 4 were subjected to CO 2 adsorption tests at 101.325kPa and 298.15K using a fully automatic specific surface area and porosity analyzer (Quantachrome Autosorb IQ). The adsorption capacity of the lamellar stacked spherical molecular sieve prepared in example 1 was 2.61mmol/g. The adsorption capacity of the lamellar stacked spherical molecular sieve prepared in example 2 was 2.72mmol/g. The adsorption capacity of the lamellar stacked spherical molecular sieve prepared in example 3 was 2.86mmol/g. The adsorption capacity of the lamellar stacked spherical molecular sieve prepared in example 4 was 2.91mmol/g. The adsorption capacity of CO 2 of the lamellar stacked spherical molecular sieve prepared in the examples 1-4 is more than 2.5mmol/g at normal temperature and normal pressure, and the adsorption effect is good. And as the addition amount of aluminum ash and crystallization time are increased, the adsorption capacity of the lamellar stacked spherical molecular sieve prepared in examples 1-4 is gradually increased, which is attributed to the improvement of the morphology regularity and the crystallinity of the molecular sieve as shown in fig. 2,4, 6 and 9-12.|[0085] The preparation method of the stacked spherical molecular sieve based on the multiple solid waste sheets and the corresponding materials and applications have the following beneficial effects:|[0086] 1. Adopting alkali fusion activated carbon-free gangue powder and aluminum ash to prepare a stacked spherical molecular sieve based on multiple solid waste slices together, wherein the raw materials are solid wastes; activated carbon-free gangue powder is obtained through carbon removal activation and alkali fusion activation treatment, so that the utilization rate of silicon-aluminum components in the gangue is improved while the preparation cost is reduced; |[0087] 2. The molecular sieve morphology is regulated and controlled through aging treatment and crystallization treatment by controlling the mass ratio of activated carbon-free gangue powder to aluminum ash powder, so that the molecular sieve with the lamellar stacking spherical shape, regular morphology and uniform size is synthesized, the specific surface area of the molecular sieve is improved through the lamellar stacking morphology, and the CO 2 adsorption capacity is remarkably improved; |[0088] 3. The spherical molecular sieve based on the multi-element solid waste lamellar stack prepared by the invention can realize the adsorption of CO 2 under the conditions of normal temperature and normal pressure, avoids the energy consumption and the increase of cost caused by high-temperature and high-pressure operation, obviously improves the applicability and the flexibility of material adsorption by CO 2 adsorption under the conditions of normal temperature and normal pressure, and has wide prospect in industrial application; |[0089] 4. The preparation method based on the multi-element solid waste sheet stacked spherical molecular sieve has the advantages of simplicity in operation, good repeatability and low cost, and is suitable for industrial popularization and application. |[0090] The foregoing is merely illustrative of the present invention, and the present invention is not limited thereto, and any changes or substitutions easily contemplated by those skilled in the art within the scope of the present invention should be included in the present invention. Therefore, the protection scope of the invention is subject to the protection scope of the claims. Family Number|(110930449)|110930449|Abstract|(CN118439627 A)|The invention relates to the technical field of CO2 adsorption materials , and relates to a preparation method of a multi - solid waste - based lamellar stacked spherical molecular sieve and a corresponding material and application , and the preparation method comprises the following steps : carrying out ball milling and crushing on coal gangue to obtain coal gangue powder , and carrying out carbon removal and activation treatment on the coal gangue powder to obtain carbon - free coal gangue powder ; the preparation method comprises the following steps : mixing carbon - free coal gangue powder with sodium hydroxide powder according to a ratio to obtain first mixed powder , and carrying out alkali fusion activation treatment on the first mixed powder to obtain activated carbon - free coal gangue powder ; the activated carbon - free coal gangue powder and aluminum ash powder are mixed according to the proportion , second mixed powder is obtained , the second mixed powder is aged with deionized water according to the proportion , and an aged material is obtained ; and performing crystallization treatment on the aged material to obtain a crystallized material , and washing and drying the crystallized material to obtain the lamellar stacked spherical molecular sieve . The molecular sieve material for adsorbing CO2 under normal temperature and pressure conditions can be prepared , the CO2 adsorption capacity is remarkably improved , the operation is simple , the repeatability is good , and the cost is low . |CPC codes|(CN118439627 A)|B01D - 053/02 |B01D - 2253/104 |B01D - 2253/10 |B01D - 2253/112 |B01D - 2257/504 |B01J - 020/18 |B01J - 020/28/019 |B01J - 020/28/035 |C01B - 039/14 |C01P - 2002/72 |C01P - 2004/03 |C01P - 2004/32 |IPC codes|(CN118439627 A)|B01D - 053/02 |B01J - 020/18 |B01J - 020/28 |B01J - 020/30 |C01B - 039/14 | Chemical engineering|Environmental technology|Materials, metallurgy B01D-053/02|B01D-2253/10|B01D-2253/104|B01D-2253/112|B01D-2257/504|B01J-020/18|B01J-020/28/019|B01J-020/28/035|C01B-039/14|C01P-2002/72|C01P-2004/03|C01P-2004/32 B01D-053/02|B01D-2253/10|B01D-2253/104|B01D-2253/112|B01D-2257/504|B01J-020/18|B01J-020/28/019|B01J-020/28/035|C01B-039/14|C01P-2002/72|C01P-2004/03|C01P-2004/32 B01D-053/02|B01J-020/18|B01J-020/28|B01J-020/30|C01B-039/14 B01D-053/02|B01J-020/18|B01J-020/28|B01J-020/30|C01B-039/14 CN114988426|CN114477213|CN107758682|CN117509661|US20220267159|CN108275695 CN114988426 101627409 WHO=Examiner SELF=N CAT=Y|CN114477213 100013238 WHO=Examiner SELF=N CAT=Y|CN107758682 78965691 WHO=Examiner SELF=N CAT=Y|CN117509661 108442770 WHO=Examiner SELF=N CAT=A|US20220267159 101375854 WHO=Examiner SELF=N CAT=A|CN108275695 80571725 WHO=Examiner SELF=N CAT=A 杜涛等: &quot;《废弃物制备CO2吸附剂的原理与应用》&quot;, 31 December 2023, 冶金工业出版社, pages: 27 - 28 (Cat. A) CN107758682; CN108275695; CN114477213; US20220267159; CN114988426; CN117509661 PENDING (CN118439627)|PENDING ALIVE (CN118439627)|ALIVE (CN118439627)|LEGAL DETAILS FOR CN118439627|Actual or expected expiration date=2044-05-06|Legal state=ALIVE|Status=PENDING|Event publication date=2024-05-06|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202410545871|Application date=2024-05-06|Standardized application number=2024CN-0545871|Event publication date=2024-08-06|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN118439627|Publication stage code=A|Publication date=2024-08-06|Standardized publication number=CN118439627|Event publication date=2024-08-06|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2024-08-23|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN118439627)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoSLG26WY8aIK1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073870820&ekey=2273&xpn=CN118439627&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=Z7VV9hYR938hLGJJxYTvFZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN118439627)|CN (CN118439627)|NAME=ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN (CN118439627)|NAME=WANG HAIRONG;BEIJING SHANGYUE IP AGENCY (GENERAL PARTNERSHIP) , REG=11723 (CN118439627)|NAME=WANG QINGPING|NAME=XU WEI|NAME=MIN JING|NAME=CAI JINGYI|NAME=YU QINGBO|NAME=WEI YONGCHENG|NAME=YUAN YUMENG 0 1 Titre: (CN118439627)|Spherical molecular sieve preparation method based on multi-element solid waste sheet layer stacking, corresponding material and application Résumé: (CN118439627)|The invention relates to the technical field of CO2 adsorption materials, and relates to a preparation method of a multi-solid waste-based lamellar stacked spherical molecular sieve and a corresponding material and application, and the preparation method comprises the following steps: carrying out ball milling and crushing on coal gangue to obtain coal gangue powder, and carrying out carbon removal and activation treatment on the coal gangue powder to obtain carbon-free coal gangue powder; the preparation method comprises the following steps: mixing carbon-free coal gangue powder with sodium hydroxide powder according to a ratio to obtain first mixed powder, and carrying out alkali fusion activation treatment on the first mixed powder to obtain activated carbon-free coal gangue powder; the activated carbon-free coal gangue powder and aluminum ash powder are mixed according to the proportion, second mixed powder is obtained, the second mixed powder is aged with deionized water according to the proportion, and an aged material is obtained; and performing crystallization treatment on the aged material to obtain a crystallized material, and washing and drying the crystallized material to obtain the lamellar stacked spherical molecular sieve. The molecular sieve material for adsorbing CO2 under normal temperature and pressure conditions can be prepared, the CO2 adsorption capacity is remarkably improved, the operation is simple, the repeatability is good, and the cost is low. 117 Abstract gpt-4o-mini no The article focuses on CO2 adsorption materials and methods for preparing molecular sieves, which do not involve accelerated weathering or mineral carbonation processes.
121 CN201711190413 CN201711190413 CN107973335 79539744 CN107973335 A 2018-05-01 [CN107973335] 2017-11-24 2017-11-24 2018-05-01 (CN107973335)|2019-12-27 (CN107973335)|Alkaline wet recovery method for mercury from waste mercury catalyst (CN107973335)|The present invention provides an alkaline wet recovery method for mercury from a waste mercury catalyst, particularly aims to recovery and reuse of a mercury catalyst which is used in petrochemical production for solving the recycling problem of mercury and reducing the risk of mercury pollution. The main points of the method comprise the steps of firstly, crushing the waste mercury catalyst (hereinafter referred to as a material), adding an alkaline leaching solution according to a certain solid-liquid ratio, performing leaching with stirring at 60-70 DEG C, filtering out the leaching residue, and depositing mercury salts. The advantages of the method comprise that the technological process is simple, the whole production process does not generate mercury steam, the removal rate of mercury is high, the residual mercury content in the leaching residue is lower than 0.08%, automated production can be extremely easily achieved, and due to the alkalinity of the leachate, corrosion to equipment and vessels is small, so the purity of the obtained mercury salts is very high, and further processing at a later stage is facilitated; and at the same time, since the temperature in the leaching conditions is only 60-70 DEG C, activated carbon after mercury removal still maintains original activity and can be used again. JIANGSU YANCHENG ENVIRONMENTAL PROTECTION TECHNOLOGY CHENGZHONG METAL CONTROL RESEARCH CENTER (CN107973335)|JIANGSU YANCHENG ENVIRONMENTAL PROTECTION TECH CHENGZHONG METAL CONTROL RESEARCH CENTER WANG DEYU|ZHANG ZHENGJIE|CHEN YANG|ZHU HEWEI (CN107973335)|WANG DEYU|ZHANG ZHENGJIE|CHEN YANG|ZHU HEWEI (CN107973335)|WANG YONG;SHENYANG KEWEI INTERNATIONAL PATENT OFFICE (CN107973335)|Compared with the prior art, the invention has the advantages that: the method has the advantages that the process is simple, and mercury vapor is not generated in the whole production process; the mercury removal rate is high, and the content of residual mercury in the leaching residue is lower than 0.08%; the automatic production can be easily realized, and the leaching solution is alkaline and has little corrosion to equipment and containers, so that the obtained mercury salt has high purity and is very beneficial to the further processing in the later period; meanwhile, the temperature in the leaching condition is only 60-70 ℃, so the activated carbon after demercuration still maintains the original activity and can be reused.|Patent CN 105154676A provides a mercury waste catalyst comprehensive treatment method, through mixing mercury waste catalyst and quick lime, boil it and process, make the active ingredient of mercury waste catalyst and quick lime take place the effect, reach the curing mercury waste catalyst purpose, improve mercury waste catalyst conversion efficiency in the distillation process, through cooling the mercury-containing steam that obtains after to the distillation, obtain the steam sediment, again with steam sediment and reactant effect, make mercury composition wherein obtain a large amount of precipitations, through ultrasonic treatment, coupling centrifugal treatment, make reactant and steam sediment effect more thorough.|The process is easy to operate, has low equipment requirement, but can only recover 60 percent of HgCl2In the presence of HgCl2Low recovery rate.|The invention has simple process, easy realization of automatic production, no mercury vapor generation in the whole production process and environmental protection; the mercury removal rate is high, the content of residual mercury in the leaching residue is lower than 0.08 percent, and the mercury removal is complete; the leaching solution is alkaline, so that the corrosion to equipment and containers is small, the purity of the obtained mercury salt is high, and the further processing in the later period is facilitated; meanwhile, the temperature in the leaching condition is only 60-70 ℃, so that the activated carbon after demercuration still maintains the original activity and can be reused, and the problem of large loss of the activated catalyst after demercuration in the prior art is solved.| (CN107973335)|1. A method for recovering mercury from waste mercury catalyst by alkaline wet method is characterized in that: the method comprises the following steps:step 1, crushing the materials to below 200 meshes, and putting the materials into a stainless steel container;step 2, adding a leaching solution according to the solid-to-liquid ratio of 1: 1.5-1: 3, and covering a container cover, wherein the leaching solution is sodium hydroxide with the concentration of 1.25-2.0 mol/L, Na2An aqueous solution with the S concentration of 0.5-1.0 mol/L;step 3, controlling the leaching temperature to be 60-70 ℃, and stirring and leaching for 2.5 hours;step 4, filter-pressing the leaching residues, and repeating the leaching residues according to the steps 1-3 once and then performing the step 5;step 5, filter-pressing the leaching residue in the step 4;step 6, adjusting the pH value of the filtrate to 9-11, introducing weak acid gas, and precipitating mercury salt in the filtrate in the form of mercury sulfide until no precipitate is generated;and 7, filtering and washing the precipitate with water to obtain mercury salt.| (CN107973335)|The invention aims to provide a method for recovering mercury from waste mercury catalyst by an alkaline wet method, so as to solve the problems in the prior art.|The invention provides a method for recovering mercury from waste mercury catalyst by an alkaline wet method, which is particularly used for recovering and reusing a catalyst-mercury catalyst used in petrochemical production so as to solve the problem of recycling of mercury and reduce the risk of mercury pollution.| (CN107973335)|WASTE MERCURY CATALYST(100,19)|RECOVERING MERCURY(100,7)|ALKALINE WET(100,5)|RECYCLING MERCURY(100,1)|LEACHING RESIDUE(87,12)|LEACHING RESIDUE FILTRATION(54,1)|LEACHING SOLUTION(53,6)|PRECIPITATING MERCURY SALT(42,2)|ALKALINE LEACHING SOLUTION(36,1)|RESIDUAL MERCURY(36,1)|MERCURY POLLUTION(35,1)|PRECIPITATE(32,8)|FILTRATE(31,10)|MERCURY SALT DEPOSITION(30,1)|LEACHING CONDITION(29,1)|LEACHING(26,10)|STAINLESS STEEL CONTAINER(26,2)|PETROCHEMICAL PRODUCTION(26,1)|CONTAINER COVER(25,2)|MERCURY SALT(24,4)|AUTOMATIC PRODUCTION(24,1)|LATE PERIOD(24,1)|LEACHING TEMPERATURE(23,6)|CORROSION(22,1)|DEMERCURATION STILL(22,1)|MERCURY REMOVAL RATE(21,1)|PURITY(21,1)|MERCURY(19,5)|AQUEOUS SOLUTION(19,3)|METHANEDIONE(17,4)|SODIUM HYDROXIDE(14,4)|WEAK ACID GAS(14,4)|MERCURY II SULFIDE(13,2)|MERCURY VAPOR(12,3)|ALKYLTHIAZOLE DICYANAMIDE(11,1)|PENTAFLUORO ETHYL SULFONAMIDES(11,1)|WASTE MERCURY CATALYST PRETREATMENT(11,1)|HGCL2THE MERCURY CATALYST(10,1)|QUATERNARY AMINOPHOSPHONATE(10,1)|SYNTHESIZING CHLOROETHENE(10,1)|METALLIC MERCURY(9,4)|FILTERED SLAG(8,2)|MERCURIC SALT(8,2)|HUGE ECONOMIC BENEFIT(8,1)|LEACHED SLAG(8,1)|MERCURY ENVIRONMENTAL FRIENDLY RECOVERY(8,1)|LEACHATE(7,4)|METHANESULFINYLMETHANE(7,2)|TETRACHLOROMETHANE(7,2)|ETHANE IMIDE(7,1)|EXTENSIVE UTILIZATION(7,1)|MERCURY RESOURCE(7,1)|SYNCHRONOUSLY RECOVERING MERCURY CHLORIDE(7,1)|ACIDIC GAS(6,4)|ELECTROLYSIS LINK(6,1)|EQUIPMENT REQUIREMENT DEFECT(6,1)|MERCURY REPLACEMENT CATALYST(6,1)|REPLACED WASTE MERCURY CATALYST(6,1)|STEAM CONDENSATION(6,1)|POLYVINYL CHLORIDE(5,7)|ACCESSORY(5,2)|MERCURY CHLORIDE VAPOR(5,2)|STAINLESS STEEL TANK(5,2)|CORROSIVITY(5,1)|DRY DISTILLATION(5,1)|MERCURIC CHLORIDE CATALYST(5,1)|RECOVERING MERCURY SALT(5,1)|TEMPERATURE2SUBLIMATING(5,1)|ACETYLENE(3,1)|ACIDIC CONDITION(3,1)|ACTIVATED CARBON MICROPORE(3,1)|AGRICULTURE(3,1)|BUBBLING(3,1)|CATALYST CHANNEL(3,1)|ELECTRICAL REDUCTION(3,1)|ENVIRONMENTAL POLLUTION(3,1)| (CN107973335)|1. A method for recovering mercury from waste mercury catalyst by alkaline wet method is characterized in that: the method comprises the following steps:|step 1, crushing the materials to below 200 meshes, and putting the materials into a stainless steel container;|step 2, adding a leaching solution according to the solid-to-liquid ratio of 1: 1.5-1: 3, and covering a container cover, wherein the leaching solution is sodium hydroxide with the concentration of 1.25-2.0 mol/L, Na2An aqueous solution with the S concentration of 0.5-1.0 mol/L;|step 3, controlling the leaching temperature to be 60-70 ℃, and stirring and leaching for 2.5 hours;|step 4, filter-pressing the leaching residues, and repeating the leaching residues according to the steps 1-3 once and then performing the step 5;|step 5, filter-pressing the leaching residue in the step 4;|step 6, adjusting the pH value of the filtrate to 9-11, introducing weak acid gas, and precipitating mercury salt in the filtrate in the form of mercury sulfide until no precipitate is generated;|and 7, filtering and washing the precipitate with water to obtain mercury salt.|2. The method of claim 1, wherein: in the step 6, the weakly acidic gas is carbon dioxide. (CN107973335)|TECHNICAL FIELD|[0002] The invention belongs to the technical field of environmental protection and non-ferrous metal recycling, and particularly relates to a method for leaching and recovering mercury salt in a waste mercury catalyst by adopting an alkaline wet method, in particular to a method for recovering mercury from a waste mercury catalyst taking activated carbon as a carrier.|BACKGROUND ART|[0004] China is a large country for producing polyvinyl chloride (PVC), and the polyvinyl chloride is widely applied to industries such as industry, building, agriculture and the like due to excellent physical and chemical properties of the polyvinyl chloride. The preparation method is generally divided into two methods: calcium carbide process and ethylene process. Because oil in China is less and coal is more, PVC produced by the calcium carbide method accounts for the main percentage and accounts for about 70 percent of the total amount of PVC. The mercuric chloride catalyst (commonly called mercury catalyst) is used as a catalyst for synthesizing Vinyl Chloride (VCM) by acetylene and hydrogen chloride gas in PVC production by a calcium carbide method, and is prepared by taking active carbon as a carrier and mercuric chloride as an active substance and loading the mercuric chloride on the surface of the active carbon. After the mercury catalyst is used for a certain period of time, the activity of the mercury catalyst is reduced and the mercury catalyst needs to be replaced, and the replaced waste mercury catalyst generally contains about 2-5% of mercury chloride.The failure of mercury catalyst is mainly caused by (1) HgCl at high temperature2Sublimating to greatly reduce the content of mercuric chloride. (2) The catalyst is poisoned. (3) Impurities in the production raw materials cover the surface of the catalyst or block the catalyst channels. Due to HgCl2The mercury catalyst is extremely toxic, volatile and soluble in water, so that the replaced mercury catalyst is easy to cause environmental pollution and potential safety hazard if stacked or stored for a long time. Moreover, the mercury resources in China are increasingly exhausted, and a large amount of mercury is imported every year. Therefore, the waste mercury catalyst is efficiently recycled, so that the mercury can be prevented from entering the environment to cause harm to human health, and huge economic benefits can be obtained.|[0005] The waste mercury catalyst is recycled mainly by the following methods: the "double salt method" uses NaCl to treat waste mercury catalyst in the presence of hydrochloric acid to make HgCl2Formation of Na2HgCl4The double salt is eluted, and then the double salt is reduced into metallic mercury by formaldehyde for recycling. The process is easy to operate, has low equipment requirement, but can only recover 60 percent of HgCl2In the presence of HgCl2Low recovery rate.|[0006] The high-temp process includes chemical pretreatment of waste mercury catalyst to obtain HgCl2And the mercury is converted into mercury oxide, then the mercury oxide is placed in a metal can, the metal can is heated to 700-800 ℃ to be decomposed into mercury vapor, and the mercury vapor is condensed to recover the metal mercury. The method has the defects of high equipment requirement, high energy consumption and the like. In addition, patent CN 102962033A discloses a method for synchronously recovering mercury chloride, metal salts and activated carbon in a waste mercury catalyst, which comprises drying the waste mercury catalyst, heating to 350-800 ℃, performing dry distillation to obtain mercury chloride vapor, recovering mercury chloride in the waste mercury catalyst by combining condensation and water solution absorption, then soaking with hot water, driving out deposits in activated carbon micropores by combining with air bubbling, recovering activated carbon gaps, drying to recover activated carbon, and filtering to recover metal salts. As the mercury chloride vapor has high corrosivity to equipment, special anticorrosive materials are required, and the defects of high energy consumption, high equipment requirement, high operation cost and the like exist.|[0007] Patent CN 104263942 a discloses a comprehensive utilization method of waste mercury catalyst, which recovers mercury salt in waste mercury catalyst by combining soaking, alkalization, leaching, reduction and filtration steps. However, this method has the following drawbacks: firstly, the water consumption is large, and the solid-liquid ratio of the soaking process reaches 1: 2-1: 2.5; secondly, the construction period is too long, wherein soaking: alkalization for 10-15 h: 3-5 h, leaching: 15-17 h, reduction: 6-13 h, subsequent filtering and other processes are carried out, so that the time is longer; furthermore, steam is required to be introduced for 15-17 hours during leaching, energy consumption is high, in addition, new water generated by steam condensation can dilute the leaching solution, and water consumption is increased; finally, calcium salt solid waste generated by adding quicklime in the alkalization step needs further treatment, so that the cost is increased.|[0008] Patent CN 104451154 a is a new technology for recovering mercury in mercury-containing catalyst by wet process, but this technology uses a large amount of organic reagents such as benzene, carbon tetrachloride, pyrrolidone, ethyl acetate, dimethyl sulfoxide, sulfolane, dimethyl imide, acetone, butanol, alkyl pyrroline pentafluoroethyl sulfonamide, 1- (1-aminoalkyl) -3-methylimidazole tetrafluoroborate, ethanolamine, L-asparagine monohydrate, ethylenediamine, hydrazine hydrate, pyridine, carbon disulfide, dimethyl sulfoxide, sulfur hexafluoride, mercaptoethanol, methylimidazole, thiourea dioxide, carbon tetrachloride, quaternary phosphoramidate, and alkylthiazole dicyanamide, and the above organic reagents are many flammable and volatile substances, and have great safety hazard during operation.|[0009] Patent CN 104372378A provides an apparatus and a method for environmental-friendly recovery of mercury and activated carbon from multiple components of waste mercury catalyst. The method adopts an electric reduction method in a chloride system of hydrochloric acid, has the defects of long construction period and the like, takes 45-60 hours only in an electrolysis link, and has higher requirements on equipment when running under an acidic condition.|[0010] Patent CN 105154676A provides a mercury waste catalyst comprehensive treatment method, through mixing mercury waste catalyst and quick lime, boil it and process, make the active ingredient of mercury waste catalyst and quick lime take place the effect, reach the curing mercury waste catalyst purpose, improve mercury waste catalyst conversion efficiency in the distillation process, through cooling the mercury-containing steam that obtains after to the distillation, obtain the steam sediment, again with steam sediment and reactant effect, make mercury composition wherein obtain a large amount of precipitations, through ultrasonic treatment, coupling centrifugal treatment, make reactant and steam sediment effect more thorough. The method has the same defects of high energy consumption, long construction period, generation of new calcium salt and solid waste and the like as in the patent CN 104263942A.|DISCLOSURE|[0011] Disclosure of Invention|[0012] The invention aims to provide a method for recovering mercury from waste mercury catalyst by an alkaline wet method, so as to solve the problems in the prior art.|[0013] The invention is realized by the following technical scheme: a method for recovering mercury from waste mercury catalyst by alkaline wet method comprises the following steps:|[0014] step 1, crushing the materials to below 200 meshes, and putting the materials into a stainless steel container;|[0015] step 2, adding a leaching solution according to the solid-to-liquid ratio of 1: 1.5-1: 3, and covering a container cover, wherein the leaching solution is sodium hydroxide with the concentration of 1.25-2.0 mol/L, Na2An aqueous solution with the S concentration of 0.5-1.0 mol/L;|[0016] step 3, controlling the leaching temperature to be 60-70 ℃, and stirring and leaching for 2.5 hours;|[0017] step 4, filter-pressing the leaching residues, and repeating the leaching residues according to the steps 1-3 once and then performing the step 5;|[0018] step 5, filter-pressing the leaching residue in the step 4;|[0019] step 6, adjusting the pH value of the filtrate to 9-11, introducing weak acid gas, and precipitating mercury salt in the filtrate in the form of mercury sulfide until no precipitate is generated;|[0020] and 7, filtering and washing the precipitate with water to obtain mercury salt.|[0021] Further: in the step 6, the weakly acidic gas is carbon dioxide.|[0022] Compared with the prior art, the invention has the advantages that: the method has the advantages that the process is simple, and mercury vapor is not generated in the whole production process; the mercury removal rate is high, and the content of residual mercury in the leaching residue is lower than 0.08%; the automatic production can be easily realized, and the leaching solution is alkaline and has little corrosion to equipment and containers, so that the obtained mercury salt has high purity and is very beneficial to the further processing in the later period; meanwhile, the temperature in the leaching condition is only 60-70 ℃, so the activated carbon after demercuration still maintains the original activity and can be reused.|INVENTION MODE|[0023] Detailed Description|[0024] The invention is further illustrated by the following specific examples.|INVENTION MODE|[0025] Example 1|[0026] The method for recovering mercury from waste mercury catalyst by alkaline wet method comprises the following steps:|[0027] step 1, crushing 200 g of materials to 200 meshes, placing the materials into a stainless steel tank, and adding 300mL of leachate;|[0028] step 2, controlling the leaching temperature to be 60 ℃, and stirring and leaching for 2.5 hours;|[0029] step 3, filter-pressing the leaching residues, and repeating the leaching residues according to the steps 1 and 2 once;|[0030] step 4, filter-pressing the leaching residue in the step 3;|[0031] step 5, adjusting the pH value of the filtrate to 10, and introducing weak acid gas until no precipitate is generated;|[0032] step 6, filtering and washing the precipitate with water to obtain mercuric salt;|[0033] and 7, combining the filtrates, and performing corresponding supplement according to the component content in the filtrate for re-leaching.|[0034] Wherein the leachate in the step 1 comprises the following components: sodium hydroxide concentration of1.3 mol/L、Na2The specific gravity of the aqueous solution with the S concentration of 0.6mol/L is calculated according to the specific gravity of water, the liquid-solid ratio (mass ratio) is 1:1.5, the leaching temperature is 60 ℃, the leaching time is 2.5 hours, and the weakly acidic gas is carbon dioxide. Through detection, the content of metallic mercury in the filtered slag is as follows: 0.072 percent.|INVENTION MODE|[0035] Specific example 2|[0036] The method for recovering mercury from waste mercury catalyst by alkaline wet method comprises the following steps:|[0037] 1. crushing 200 g of materials with 200 meshes, placing the materials into a stainless steel tank, and adding 400mL of leachate;|[0038] 2. controlling the leaching temperature to be 65 ℃, and stirring and leaching for 2.5 hours;|[0039] 3. filter-pressing the leaching residue, and repeating the leaching residue according to the steps 1 and 2 once;|[0040] 4. filter-pressing the leached slag in the step 3;|[0041] 5. adjusting the pH value of the filtrate, and introducing weak acid gas until no precipitate is generated;|[0042] 6. filtering and washing the precipitate with water to obtain mercuric salt;|[0043] 7. combining the filtrates, and performing corresponding supplement according to the component content in the filtrate for further leaching.|[0044] The composition of the leachate in the step 1 is as follows: the concentration of sodium hydroxide is 1.25 mol/L, Na2The S concentration is 0.7mol/L, the liquid-solid ratio is 1:2, the leaching temperature is 65 ℃, the leaching time is 2.5 hours, and the weakly acidic gas is carbon dioxide. Through detection, the content of metallic mercury in the filtered slag is as follows: 0.076 percent.|[0045] The invention has simple process, easy realization of automatic production, no mercury vapor generation in the whole production process and environmental protection; the mercury removal rate is high, the content of residual mercury in the leaching residue is lower than 0.08 percent, and the mercury removal is complete; the leaching solution is alkaline, so that the corrosion to equipment and containers is small, the purity of the obtained mercury salt is high, and the further processing in the later period is facilitated; meanwhile, the temperature in the leaching condition is only 60-70 ℃, so that the activated carbon after demercuration still maintains the original activity and can be reused, and the problem of large loss of the activated catalyst after demercuration in the prior art is solved. (CN107973335)|TECHNICAL FIELD|[0002] The invention belongs to the technical field of environmental protection and non-ferrous metal recycling, and particularly relates to a method for leaching and recovering mercury salt in a waste mercury catalyst by adopting an alkaline wet method, in particular to a method for recovering mercury from a waste mercury catalyst taking activated carbon as a carrier.|BACKGROUND ART|[0004] China is a large country for producing polyvinyl chloride (PVC), and the polyvinyl chloride is widely applied to industries such as industry, building, agriculture and the like due to excellent physical and chemical properties of the polyvinyl chloride. The preparation method is generally divided into two methods: calcium carbide process and ethylene process. Because oil in China is less and coal is more, PVC produced by the calcium carbide method accounts for the main percentage and accounts for about 70 percent of the total amount of PVC. The mercuric chloride catalyst (commonly called mercury catalyst) is used as a catalyst for synthesizing Vinyl Chloride (VCM) by acetylene and hydrogen chloride gas in PVC production by a calcium carbide method, and is prepared by taking active carbon as a carrier and mercuric chloride as an active substance and loading the mercuric chloride on the surface of the active carbon. After the mercury catalyst is used for a certain period of time, the activity of the mercury catalyst is reduced and the mercury catalyst needs to be replaced, and the replaced waste mercury catalyst generally contains about 2-5% of mercury chloride.The failure of mercury catalyst is mainly caused by (1) HgCl at high temperature2Sublimating to greatly reduce the content of mercuric chloride. (2) The catalyst is poisoned. (3) Impurities in the production raw materials cover the surface of the catalyst or block the catalyst channels. Due to HgCl2The mercury catalyst is extremely toxic, volatile and soluble in water, so that the replaced mercury catalyst is easy to cause environmental pollution and potential safety hazard if stacked or stored for a long time. Moreover, the mercury resources in China are increasingly exhausted, and a large amount of mercury is imported every year. Therefore, the waste mercury catalyst is efficiently recycled, so that the mercury can be prevented from entering the environment to cause harm to human health, and huge economic benefits can be obtained.|[0005] The waste mercury catalyst is recycled mainly by the following methods: the "double salt method" uses NaCl to treat waste mercury catalyst in the presence of hydrochloric acid to make HgCl2Formation of Na2HgCl4The double salt is eluted, and then the double salt is reduced into metallic mercury by formaldehyde for recycling. The process is easy to operate, has low equipment requirement, but can only recover 60 percent of HgCl2In the presence of HgCl2Low recovery rate.|[0006] The high-temp process includes chemical pretreatment of waste mercury catalyst to obtain HgCl2And the mercury is converted into mercury oxide, then the mercury oxide is placed in a metal can, the metal can is heated to 700-800 ℃ to be decomposed into mercury vapor, and the mercury vapor is condensed to recover the metal mercury. The method has the defects of high equipment requirement, high energy consumption and the like. In addition, patent CN 102962033A discloses a method for synchronously recovering mercury chloride, metal salts and activated carbon in a waste mercury catalyst, which comprises drying the waste mercury catalyst, heating to 350-800 ℃, performing dry distillation to obtain mercury chloride vapor, recovering mercury chloride in the waste mercury catalyst by combining condensation and water solution absorption, then soaking with hot water, driving out deposits in activated carbon micropores by combining with air bubbling, recovering activated carbon gaps, drying to recover activated carbon, and filtering to recover metal salts. As the mercury chloride vapor has high corrosivity to equipment, special anticorrosive materials are required, and the defects of high energy consumption, high equipment requirement, high operation cost and the like exist.|[0007] Patent CN 104263942 a discloses a comprehensive utilization method of waste mercury catalyst, which recovers mercury salt in waste mercury catalyst by combining soaking, alkalization, leaching, reduction and filtration steps. However, this method has the following drawbacks: firstly, the water consumption is large, and the solid-liquid ratio of the soaking process reaches 1: 2-1: 2.5; secondly, the construction period is too long, wherein soaking: alkalization for 10-15 h: 3-5 h, leaching: 15-17 h, reduction: 6-13 h, subsequent filtering and other processes are carried out, so that the time is longer; furthermore, steam is required to be introduced for 15-17 hours during leaching, energy consumption is high, in addition, new water generated by steam condensation can dilute the leaching solution, and water consumption is increased; finally, calcium salt solid waste generated by adding quicklime in the alkalization step needs further treatment, so that the cost is increased.|[0008] Patent CN 104451154 a is a new technology for recovering mercury in mercury-containing catalyst by wet process, but this technology uses a large amount of organic reagents such as benzene, carbon tetrachloride, pyrrolidone, ethyl acetate, dimethyl sulfoxide, sulfolane, dimethyl imide, acetone, butanol, alkyl pyrroline pentafluoroethyl sulfonamide, 1- (1-aminoalkyl) -3-methylimidazole tetrafluoroborate, ethanolamine, L-asparagine monohydrate, ethylenediamine, hydrazine hydrate, pyridine, carbon disulfide, dimethyl sulfoxide, sulfur hexafluoride, mercaptoethanol, methylimidazole, thiourea dioxide, carbon tetrachloride, quaternary phosphoramidate, and alkylthiazole dicyanamide, and the above organic reagents are many flammable and volatile substances, and have great safety hazard during operation.|[0009] Patent CN 104372378A provides an apparatus and a method for environmental-friendly recovery of mercury and activated carbon from multiple components of waste mercury catalyst. The method adopts an electric reduction method in a chloride system of hydrochloric acid, has the defects of long construction period and the like, takes 45-60 hours only in an electrolysis link, and has higher requirements on equipment when running under an acidic condition.|[0010] Patent CN 105154676A provides a mercury waste catalyst comprehensive treatment method, through mixing mercury waste catalyst and quick lime, boil it and process, make the active ingredient of mercury waste catalyst and quick lime take place the effect, reach the curing mercury waste catalyst purpose, improve mercury waste catalyst conversion efficiency in the distillation process, through cooling the mercury-containing steam that obtains after to the distillation, obtain the steam sediment, again with steam sediment and reactant effect, make mercury composition wherein obtain a large amount of precipitations, through ultrasonic treatment, coupling centrifugal treatment, make reactant and steam sediment effect more thorough. The method has the same defects of high energy consumption, long construction period, generation of new calcium salt and solid waste and the like as in the patent CN 104263942A.|DISCLOSURE|[0011] Disclosure of Invention|[0012] The invention aims to provide a method for recovering mercury from waste mercury catalyst by an alkaline wet method, so as to solve the problems in the prior art.|[0013] The invention is realized by the following technical scheme: a method for recovering mercury from waste mercury catalyst by alkaline wet method comprises the following steps:|[0014] step 1, crushing the materials to below 200 meshes, and putting the materials into a stainless steel container;|[0015] step 2, adding a leaching solution according to the solid-to-liquid ratio of 1: 1.5-1: 3, and covering a container cover, wherein the leaching solution is sodium hydroxide with the concentration of 1.25-2.0 mol/L, Na2An aqueous solution with the S concentration of 0.5-1.0 mol/L;|[0016] step 3, controlling the leaching temperature to be 60-70 ℃, and stirring and leaching for 2.5 hours;|[0017] step 4, filter-pressing the leaching residues, and repeating the leaching residues according to the steps 1-3 once and then performing the step 5;|[0018] step 5, filter-pressing the leaching residue in the step 4;|[0019] step 6, adjusting the pH value of the filtrate to 9-11, introducing weak acid gas, and precipitating mercury salt in the filtrate in the form of mercury sulfide until no precipitate is generated;|[0020] and 7, filtering and washing the precipitate with water to obtain mercury salt.|[0021] Further: in the step 6, the weakly acidic gas is carbon dioxide.|[0022] Compared with the prior art, the invention has the advantages that: the method has the advantages that the process is simple, and mercury vapor is not generated in the whole production process; the mercury removal rate is high, and the content of residual mercury in the leaching residue is lower than 0.08%; the automatic production can be easily realized, and the leaching solution is alkaline and has little corrosion to equipment and containers, so that the obtained mercury salt has high purity and is very beneficial to the further processing in the later period; meanwhile, the temperature in the leaching condition is only 60-70 ℃, so the activated carbon after demercuration still maintains the original activity and can be reused.|INVENTION MODE|[0023] Detailed Description|[0024] The invention is further illustrated by the following specific examples.|INVENTION MODE|[0025] Example 1|[0026] The method for recovering mercury from waste mercury catalyst by alkaline wet method comprises the following steps:|[0027] step 1, crushing 200 g of materials to 200 meshes, placing the materials into a stainless steel tank, and adding 300mL of leachate;|[0028] step 2, controlling the leaching temperature to be 60 ℃, and stirring and leaching for 2.5 hours;|[0029] step 3, filter-pressing the leaching residues, and repeating the leaching residues according to the steps 1 and 2 once;|[0030] step 4, filter-pressing the leaching residue in the step 3;|[0031] step 5, adjusting the pH value of the filtrate to 10, and introducing weak acid gas until no precipitate is generated;|[0032] step 6, filtering and washing the precipitate with water to obtain mercuric salt;|[0033] and 7, combining the filtrates, and performing corresponding supplement according to the component content in the filtrate for re-leaching.|[0034] Wherein the leachate in the step 1 comprises the following components: sodium hydroxide concentration of1.3 mol/L、Na2The specific gravity of the aqueous solution with the S concentration of 0.6mol/L is calculated according to the specific gravity of water, the liquid-solid ratio (mass ratio) is 1:1.5, the leaching temperature is 60 ℃, the leaching time is 2.5 hours, and the weakly acidic gas is carbon dioxide. Through detection, the content of metallic mercury in the filtered slag is as follows: 0.072 percent.|INVENTION MODE|[0035] Specific example 2|[0036] The method for recovering mercury from waste mercury catalyst by alkaline wet method comprises the following steps:|[0037] 1. crushing 200 g of materials with 200 meshes, placing the materials into a stainless steel tank, and adding 400mL of leachate;|[0038] 2. controlling the leaching temperature to be 65 ℃, and stirring and leaching for 2.5 hours;|[0039] 3. filter-pressing the leaching residue, and repeating the leaching residue according to the steps 1 and 2 once;|[0040] 4. filter-pressing the leached slag in the step 3;|[0041] 5. adjusting the pH value of the filtrate, and introducing weak acid gas until no precipitate is generated;|[0042] 6. filtering and washing the precipitate with water to obtain mercuric salt;|[0043] 7. combining the filtrates, and performing corresponding supplement according to the component content in the filtrate for further leaching.|[0044] The composition of the leachate in the step 1 is as follows: the concentration of sodium hydroxide is 1.25 mol/L, Na2The S concentration is 0.7mol/L, the liquid-solid ratio is 1:2, the leaching temperature is 65 ℃, the leaching time is 2.5 hours, and the weakly acidic gas is carbon dioxide. Through detection, the content of metallic mercury in the filtered slag is as follows: 0.076 percent.|[0045] The invention has simple process, easy realization of automatic production, no mercury vapor generation in the whole production process and environmental protection; the mercury removal rate is high, the content of residual mercury in the leaching residue is lower than 0.08 percent, and the mercury removal is complete; the leaching solution is alkaline, so that the corrosion to equipment and containers is small, the purity of the obtained mercury salt is high, and the further processing in the later period is facilitated; meanwhile, the temperature in the leaching condition is only 60-70 ℃, so that the activated carbon after demercuration still maintains the original activity and can be reused, and the problem of large loss of the activated catalyst after demercuration in the prior art is solved. Family Number|(79539744)|79539744|Abstract|(CN107973335 A)|The present invention provides an alkaline wet recovery method for mercury from a waste mercury catalyst , particularly aims to recovery and reuse of a mercury catalyst which is used in petrochemical production for solving the recycling problem of mercury and reducing the risk of mercury pollution . The main points of the method comprise the steps of firstly , crushing the waste mercury catalyst ( hereinafter referred to as a material ) , adding an alkaline leaching solution according to a certain solid - liquid ratio , performing leaching with stirring at 60-70 DEG C , filtering out the leaching residue , and depositing mercury salts . The advantages of the method comprise that the technological process is simple , the whole production process does not generate mercury steam , the removal rate of mercury is high , the residual mercury content in the leaching residue is lower than 0.08%, automated production can be extremely easily achieved , and due to the alkalinity of the leachate , corrosion to equipment and vessels is small , so the purity of the obtained mercury salts is very high , and further processing at a later stage is facilitated ; and at the same time , since the temperature in the leaching conditions is only 60-70 DEG C , activated carbon after mercury removal still maintains original activity and can be used again . |CPC codes|(CN107973335 A)|C01G - 013/00 |IPC codes|(CN107973335 A)|C01G - 013/00 | Materials, metallurgy C01G-013/00 C01G-013/00 C01G-013/00 C01G-013/00 CN111268718B CN111268718B 89234204 WHO=Examiner SELF=N CN107312940|CN104032139|CN107012329|CN104263942 CN107312940 77693271 WHO=Examiner SELF=N CAT=Y|CN104032139 67393286 WHO=Examiner SELF=N CAT=Y|CN107012329 76928845 WHO=Examiner SELF=N CAT=A|CN104263942 68319767 WHO=Examiner SELF=N CAT=A CN104032139; CN104263942; CN107012329; CN107312940 LAPSED (CN107973335)|LAPSED DEAD (CN107973335)|DEAD (CN107973335)|LEGAL DETAILS FOR CN107973335|Actual or expected expiration date=2019-12-27|Legal state=DEAD|Status=LAPSED|Event publication date=2017-11-24|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201711190413|Application date=2017-11-24|Standardized application number=2017CN-1190413|Event publication date=2018-05-01|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN107973335|Publication stage code=A|Publication date=2018-05-01|Standardized publication number=CN107973335|Event publication date=2018-05-01|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2018-05-25|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2019-12-27|Event code=CN/WD01|Event indicator=Neg|Event group=Event indicating Not In Force|Patent application deemed withdrawn after publication https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjkigpRnnMODb1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=kqFpt3f38lsXpQg7OsDN%252F5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN107973335)|NAME=WANG YONG;SHENYANG KEWEI INTERNATIONAL PATENT OFFICE (CN107973335)|NAME=WANG DEYU|NAME=ZHANG ZHENGJIE|NAME=CHEN YANG|NAME=ZHU HEWEI 0 1 Titre: (CN107973335)|Alkaline wet recovery method for mercury from waste mercury catalyst Résumé: (CN107973335)|The present invention provides an alkaline wet recovery method for mercury from a waste mercury catalyst, particularly aims to recovery and reuse of a mercury catalyst which is used in petrochemical production for solving the recycling problem of mercury and reducing the risk of mercury pollution. The main points of the method comprise the steps of firstly, crushing the waste mercury catalyst (hereinafter referred to as a material), adding an alkaline leaching solution according to a certain solid-liquid ratio, performing leaching with stirring at 60-70 DEG C, filtering out the leaching residue, and depositing mercury salts. The advantages of the method comprise that the technological process is simple, the whole production process does not generate mercury steam, the removal rate of mercury is high, the residual mercury content in the leaching residue is lower than 0.08%, automated production can be extremely easily achieved, and due to the alkalinity of the leachate, corrosion to equipment and vessels is small, so the purity of the obtained mercury salts is very high, and further processing at a later stage is facilitated; and at the same time, since the temperature in the leaching conditions is only 60-70 DEG C, activated carbon after mercury removal still maintains original activity and can be used again. 122 Abstract gpt-4o-mini no The article focuses on a method for recovering mercury from waste catalysts, which does not relate to accelerated weathering or CO₂ capture.
122 CN202311039076 CN202311039076 CN117046398 107276761 CN117046398 A 2023-11-14 [CN117046398] 2023-08-17 2023-08-17 2023-11-14 (CN117046398)|2043-08-17 (CN117046398)|Process and equipment for preparing light aromatic hydrocarbon and co-producing methanol through acetylene trimerization through biomass microwave conversion (CN117046398)|The invention belongs to the technical field of biomass treatment, and particularly relates to a process for preparing light aromatic hydrocarbon and co-producing methanol through biomass microwave conversion acetylene trimerization, which comprises the following steps: (1) crushing and pretreating biomass; (2) carrying out anaerobic fermentation on the pretreated biomass particles to generate methane and carbon dioxide; (3) drying, purifying and separating methane and carbon dioxide; (4) performing microwave reaction on methane to obtain acetylene, and performing trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon; and performing methanol synthesis reaction on the hydrogen generated in the step (4) and the carbon dioxide separated in the step (3) to obtain methanol. According to the process, anaerobic fermentation, microwave conversion, acetylene trimerization and methanol synthesis processes are coupled, biomass is directly converted into light aromatic hydrocarbon compounds, a bulk chemical methanol is co-produced, a carbon sequestration effect is achieved, and the problems of solid waste recycling and quality improvement are effectively solved. CECEP ENGINEERING TECHNOLOGY RESEARCH INSTITUTE (CN117046398)|CECEP ENG TECH RES INST CO LTD ([CN]) LI QINGYUAN|XU SHIPEI|LU JIANWEN|WANG CHAO (CN117046398)|LI QINGYUAN|XU SHIPEI|LU JIANWEN|WANG CHAO (CN117046398)|ZHU DONG;CHONG QING CUI ZHI BANG CHENG ZHUAN LI DAI LI SHI WU SUO (PU TONG HE HUO)|Reg. Nb: 50231 (CN117046398)|The main advantages are as follows:| (CN117046398)|1. A process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwaves is characterized by comprising the following steps:(1) Crushing biomass and preprocessing;(2) Anaerobic fermentation is carried out on the pretreated biomass particles to generate methane and carbon dioxide;(3) Drying, purifying and separating methane and carbon dioxide;(4) Carrying out microwave reaction on methane to obtain acetylene, and carrying out trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon;(5) And (3) carrying out a methanol synthesis reaction on the hydrogen generated in the step (4) and the carbon dioxide separated in the step (3) to obtain methanol.|7. The equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass through microwaves is characterized in that: comprises a pretreatment device, an anaerobic fermentation device, a methane microwave conversion device, an acetylene trimerization reaction device and a methanol synthesis reaction device which are sequentially arranged; wherein,the pretreatment device is used for soaking biomass particles in alkali liquor and removing lignin;the anaerobic fermentation device is used for carrying out anaerobic fermentation on biomass particles to generate methane and carbon dioxide;the methane microwave conversion device is used for converting methane into acetylene;the acetylene trimerization reaction device is used for converting acetylene into light aromatic hydrocarbon;the methanol synthesis reaction device is used for preparing the methanol from the hydrogen and the carbon dioxide through the methanol synthesis reaction.| (CN117046398)|The application aims to provide a biomass conversion process for solving the problem of low economic value of methane generated in the existing biomass anaerobic fermentation. In order to solve the problems, the application provides a process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwave, which comprises the following steps:|The application also aims to provide equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwave, which comprises a pretreatment device, an anaerobic fermentation device, a methane microwave conversion device, an acetylene trimerization reaction device and a methanol synthesis reaction device which are sequentially arranged; wherein,| (CN117046398)|LIGHT AROMATIC HYDROCARBON(100,30)|METHANOL(100,26)|CONVERTING ACETYLENE(100,17)|TRIMERIZING BIOMASS(100,8)|EQUIPMENT(100,7)|MICROWAVE(100,5)|ANAEROBIC FERMENTATION(87,24)|ACETYLENE TRIMERIZATION REACTION(67,6)|TRIMERIZATION REACTION(57,11)|PRETREATED BIOMASS PARTICLE(50,6)|BIOMASS ANAEROBIC FERMENTATION(49,2)|CRUSHING BIOMASS(42,4)|SOAKING BIOMASS PARTICLE(38,3)|METHANOL SYNTHESIS REACTION(35,15)|METHANE(34,37)|METHANE SEPARATION TOWER(33,8)|PRETREATMENT(32,9)|ACETYLENE(30,19)|CRUSHED BIOMASS PARTICLE(26,2)|EMERGENCY PIPELINE(24,1)|MICROWAVE REACTION(23,5)|BIOMASS PARTICLE(22,6)|ALKALI LIQUOR(21,5)|SYNTHESIS REACTION(20,15)|PREPROCESSING(20,4)|CONVERT BIOMASS(19,2)|CARBON DIOXIDE(18,37)|BIOMASS TREATMENT(16,2)|CARBON DIOXIDE SEPARATION TOWER(14,7)|ANAEROBIC FERMENTATION TANK(14,5)|DRYING TOWER(14,5)|METHANE ECONOMIC VALUE(14,1)|ZN ZR CATALYST(13,3)|BIOMASS CONVERSION(13,1)|METHANE STORAGE TANK(12,7)|INCINERATION(12,4)|CARBON DIOXIDE SEPARATED(12,3)|SOLID WASTE RECYCLING(12,1)|LIGNIN(10,5)|ACETYLENE TRIMERIZATION REACTOR(10,2)|NAOH SOLUTION(9,2)|BIOMASS PARTICLE ANAEROBIC FERMENTATION(9,1)|PRETREATMENT TANK(8,5)|BIOMASS CONVERSION(8,1)|RENEWABLE BIOMASS RESOURCE(8,1)|REACTION TEMPERATURE(7,6)|BULK CHEMICAL METHANOL(7,5)|HYDROGEN GENERATION(7,2)|METHANE MICROWAVE CONVERSION(7,2)|METHANOL SYNTHESIS(7,2)|MOLECULAR SIEVE(7,2)|ECONOMIC VALUE(7,1)|FERMENTATION TANK STIRRING PADDLE(7,1)|NONRENEWABLE PETROLEUM RESOURCE(7,1)|MICROWAVE REACTOR(6,3)|GAS GENERATION(6,2)|BIOMASS COMPREHENSIVE UTILIZATION(6,1)|BYPRODUCT METHANE DECOMPOSITION(6,1)|QUALITY IMPROVEMENT(6,1)|CARRYING OUT ANAEROBIC FERMENTATION(5,3)|SCREW FEEDER(5,3)|ACETYLENE YIELD(5,2)|HYDROGEN SEPARATION TOWER(5,2)|MICRO WAVE CONVERSION(5,2)|ALKALI LIQUOR RECOVERY TANK(5,1)|NONRENEWABLE RESOURCE(5,1)|REACTION SPACE VELOCITY(4,3)|ALKALI LIQUOR TANK(4,1)|EXTENSIVE UTILIZATION(4,1)|METHANOL SYNTHESIS REACTOR(4,1)|HYDROGEN STORAGE TANK(3,8)|CARBON DIOXIDE STORAGE TANK(3,5)|ABNORMAL CONDITION(3,2)|EMERGENCY(3,2)|ADJUSTABLE DEFORMATION(3,1)|BIOMASS ANAEROBIC FERMENTATION(3,1)|METHANE SEPARATION COLUMN(3,1)|REALIZING CARBON PEAK(3,1)|REGULAR CHANNEL MANUFACTURE(3,1)|ALKALI SOLUTION RECYCLING TANK(2,1)|BYPRODUCT CARBON DIOXIDE(2,1)|CARBON NEUTRALIZATION(2,1)| (CN117046398)|1. A process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwaves is characterized by comprising the following steps:|(1) Crushing biomass and preprocessing;|(2) Anaerobic fermentation is carried out on the pretreated biomass particles to generate methane and carbon dioxide;|(3) Drying, purifying and separating methane and carbon dioxide;|(4) Carrying out microwave reaction on methane to obtain acetylene, and carrying out trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon;|(5) And (3) carrying out a methanol synthesis reaction on the hydrogen generated in the step (4) and the carbon dioxide separated in the step (3) to obtain methanol.|2. The process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerization through biomass microwaves according to claim 1, which is characterized in that: the pretreatment in the step (1) comprises the step of putting the crushed biomass particles into NaOH solution for soaking for 24 hours.|3. The process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerization through biomass microwaves according to claim 1, which is characterized in that: in the step (2), the temperature of the reaction system is maintained at 35 ℃, and the pH is 6.8-7.2 until the generated gas amount is obviously reduced.|4. The process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerization through biomass microwaves according to claim 1, which is characterized in that: and (3) purifying the generated hydrogen through pressure swing adsorption after the step (4).|5. The process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerization through biomass microwaves according to claim 1, which is characterized in that: in the step (4), the trimerization reaction adopts a molecular sieve to load a noble metal-based catalyst, and the reaction space velocity is 500h -1 The reaction temperature was 500 ℃.|6. The process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerization through biomass microwaves according to claim 1, which is characterized in that: the methanol synthesis reaction in the step (5) adopts a Zn-Zr catalyst, the reaction temperature is 210 ℃, and the pressure is 8Mpa.|7. The equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass through microwaves is characterized in that: comprises a pretreatment device, an anaerobic fermentation device, a methane microwave conversion device, an acetylene trimerization reaction device and a methanol synthesis reaction device which are sequentially arranged; wherein,|the pretreatment device is used for soaking biomass particles in alkali liquor and removing lignin;|the anaerobic fermentation device is used for carrying out anaerobic fermentation on biomass particles to generate methane and carbon dioxide;|the methane microwave conversion device is used for converting methane into acetylene;|the acetylene trimerization reaction device is used for converting acetylene into light aromatic hydrocarbon;|the methanol synthesis reaction device is used for preparing the methanol from the hydrogen and the carbon dioxide through the methanol synthesis reaction.|8. The device for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerization through biomass microwaves according to claim 7, wherein the device is characterized in that: and a drying tower, a carbon dioxide separation tower and a methane separation tower are sequentially arranged behind the anaerobic fermentation device, and the carbon dioxide separation tower and the methane separation tower are respectively connected with a carbon dioxide storage tank and a methane storage tank.|9. The device for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerization through biomass microwaves according to claim 7, wherein the device is characterized in that: and a gas outlet of the methane microwave conversion device is connected with a pressure swing adsorption device and a hydrogen storage tank.|10. The device for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerization through biomass microwaves according to claim 8, wherein the device is characterized in that: the methane storage tank and the methane separation tower are also provided with emergency pipelines leading to the incineration device. (CN117046398)|TECHNICAL FIELD|[0001] The application belongs to the technical field of biomass treatment, and particularly relates to a process and equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwaves.|BACKGROUND ART|[0002] Light aromatic compounds (benzene, toluene, xylene and the like) are used as important basic chemical raw materials for various chemical products. Generally, the compounds are mainly derived from non-renewable petroleum resources, and a part of the compounds are derived from coal chemical processes, but China also has the characteristics of lean oil and less gas, so that development of an alternative light aromatic hydrocarbon process route has strong practical significance.|[0003] Renewable biomass resources can not only obtain light aromatic hydrocarbon through a series of thermocatalytic processes, but also realize the recycling and high value-added utilization of biomass, and are also considered as one of important ways for realizing carbon peak and carbon neutralization in the early days, so that the method accords with the development trend of the current society.|DISCLOSURE|Disclosure of Invention|[0004] The application aims to provide a biomass conversion process for solving the problem of low economic value of methane generated in the existing biomass anaerobic fermentation.|[0005] In order to solve the problems, the application provides a process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwave, which comprises the following steps:|[0006] (1) Crushing biomass and preprocessing;|[0007] (2) Filtering the pretreated biomass particles, and performing anaerobic fermentation to generate methane and carbon dioxide;|[0008] (3) Drying, purifying and separating methane and carbon dioxide;|[0009] (4) Carrying out microwave reaction on methane to obtain acetylene, and carrying out trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon;|[0010] (5) And (3) carrying out a methanol synthesis reaction on the hydrogen generated in the step (4) and the carbon dioxide separated in the step (3) to obtain methanol.|[0011] The biomass is subjected to anaerobic fermentation to obtain methane, the methane can be converted into acetylene through microwaves, and then the acetylene can obtain light aromatic hydrocarbon compounds through a thermocatalytic process under the condition of a catalyst, so that the utilization value of the biomass is improved. In addition, a great amount of hydrogen is generated in the process of generating acetylene through methane microwave conversion, and a part of carbon dioxide is generated as a byproduct in the biomass anaerobic fermentation process besides a great amount of methane, and the part of carbon dioxide is combined with the hydrogen generated by methane decomposition to generate bulk chemicals of methanol in the presence of a catalyst, so that the methane generated by biomass anaerobic fermentation can be converted into light aromatic chemical products in the process, and the value of the light aromatic chemical products is improved; the byproduct carbon dioxide and hydrogen can be converted into bulk chemical methanol, and a new path is opened up for upgrading and comprehensive utilization of biomass.|[0012] Preferably, in order to facilitate the subsequent anaerobic fermentation of the biomass particles, the pretreatment in the step (1) comprises soaking the crushed biomass particles in NaOH solution for 24 hours to remove lignin better.|[0013] In the step (2), the temperature of the reaction system is maintained at 35 ℃ and the pH is maintained at 6.8-7.2 until the amount of generated gas is obviously reduced, and residues are removed and pretreated biomass particles are added again in order to improve the efficiency of anaerobic fermentation.|[0014] In a preferred scheme, in order to better purify the generated hydrogen, the subsequent methanol synthesis reaction is conveniently and smoothly carried out, and the hydrogen generated by pressure swing adsorption purification is carried out after the step (4).|[0015] In order to ensure efficient methanol synthesis, the methanol synthesis reaction in the step (5) adopts a Zn-Zr catalyst, wherein the reaction temperature is 210 ℃ and the pressure is 8Mpa.|[0016] The application also aims to provide equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwave, which comprises a pretreatment device, an anaerobic fermentation device, a methane microwave conversion device, an acetylene trimerization reaction device and a methanol synthesis reaction device which are sequentially arranged; wherein,|[0017] the pretreatment device is used for soaking biomass particles in alkali liquor and removing lignin;|[0018] the anaerobic fermentation device is used for carrying out anaerobic fermentation on biomass particles to generate methane and carbon dioxide;|[0019] the methane microwave conversion device is used for converting methane into acetylene;|[0020] the acetylene trimerization reaction device is used for converting acetylene into light aromatic hydrocarbon;|[0021] a methanol synthesis reaction device for preparing the hydrogen and the carbon dioxide into the methanol through the methanol synthesis reaction|[0022] As a preferable scheme, a drying tower, a carbon dioxide separation tower and a methane separation tower are further arranged behind the anaerobic fermentation device in sequence, and the carbon dioxide separation tower and the methane separation tower are respectively connected with a carbon dioxide storage tank and a methane storage tank.|[0023] As a preferable scheme, a gas outlet of the methane microwave conversion device is connected with a pressure swing adsorption device and a hydrogen storage tank.|[0024] Preferably, in order to avoid the risk of occurrence of abnormal conditions, the methane tank and the methane separation tower are further provided with emergency pipes leading to the incineration device.|[0025] The method is coupled with anaerobic fermentation, microwave conversion, acetylene trimerization and methanol synthesis processes, and directly converts biomass into light aromatic hydrocarbon compounds and combines with bulk chemicals methanol. The process can not only effectively solve the problem that light aromatic hydrocarbon is derived from renewable resources, but also coproduce and produce bulk chemicals methanol, plays a role in carbon fixation, and effectively solves the problems of recycling and upgrading of solid wastes. The main advantages are as follows:|[0026] (1) The application couples a plurality of processes together and is continuously operated to finally obtain the light aromatic hydrocarbon chemical raw material and bulk chemical methanol, thereby expanding the source of light aromatic hydrocarbon, converting non-renewable resources into renewable resources, fully utilizing carbon dioxide and playing a role of carbon fixation.|[0027] (2) The methane in the application generates a large amount of acetylene under the condition of microwave reaction, and the product not only can be used for synthesizing light aromatic compounds by trimerization, but also can be used for synthesizing other high-added-value chemicals according to different requirements, such as specific development of fine chemicals such as ethers, ketones, alcohols and the like with high added value, and has strong adjustable deformation.|[0028] (3) The application fully utilizes the carbon dioxide gas and a large amount of hydrogen generated by methane decomposition of byproducts in the reaction process, combines the characteristics of the reaction process, synthesizes a large amount of chemical methanol under the action of the catalyst, fully utilizes the byproducts, and forms a closed loop in the process from biomass to light aromatic hydrocarbon and methanol.|DRAWINGS DESCRIPTION|[0029] In order to more clearly illustrate embodiments of the present application or the prior art, the drawings that are required for the description of the embodiments or the prior art will be briefly described, and it is apparent that the drawings in the description below are some embodiments of the present application.|[0030] Fig. 1 shows an apparatus for producing light aromatic hydrocarbons and co-producing methanol by converting acetylene and trimerizing biomass by microwave in this example.|[0031] The drawings include: l-1, a screw feeder; j-1, alkali liquor tank 1; j-2, an alkali liquor recovery tank 1; p-1, a pretreatment tank; r-1 is an anaerobic fermentation tank; d-1, a drying tower; s-1, a carbon dioxide separation tower; s-2, a methane separation tower; s-3, a hydrogen separation tower; c-1, a carbon dioxide storage tank; c-2, a methane storage tank; c-3, a hydrogen storage tank; r-2 is a microwave reactor; r-3 is an acetylene trimerization reactor; r-4 is a methanol synthesis reactor.|INVENTION MODE|Detailed Description|[0032] The following examples are illustrative of the application and are not intended to limit the scope of the application. The specific techniques or conditions are not identified in the examples and are described in the literature in this field or are carried out in accordance with the product specifications.|[0033] In the description of the present application, unless otherwise indicated, the terms "upper," "lower," and the like refer to an orientation or state relationship based on that shown in the drawings, for convenience of description and simplicity of description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus should not be construed as limiting the application.|[0034] In the following examples, the equipment and the like used were conventional products available for purchase by a regular channel manufacturer, without specifying the manufacturer. The methods are conventional methods unless otherwise specified, and the starting materials are commercially available from the public sources unless otherwise specified.|[0035] Example 1|[0036] As shown in fig. 1, the embodiment provides a process and equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwave, wherein the equipment comprises a pretreatment device, an anaerobic fermentation device, a methane microwave conversion device, an acetylene trimerization reaction device and a methanol synthesis reaction device which are sequentially arranged; wherein,|[0037] the pretreatment device is used for soaking biomass particles in alkali liquor and removing lignin;|[0038] the anaerobic fermentation device is used for carrying out anaerobic fermentation on biomass particles to generate methane and carbon dioxide;|[0039] the methane microwave conversion device is used for converting methane into acetylene;|[0040] the acetylene trimerization reaction device is used for converting acetylene into light aromatic hydrocarbon;|[0041] the methanol synthesis reaction device is used for preparing the methanol from the hydrogen and the carbon dioxide through the methanol synthesis reaction.|[0042] Specifically, the pretreatment device adopts a pretreatment tank P-1, and crushed biomass is supplied to the pretreatment tank P-1 through a screw feeder L-1; the method comprises the steps of supplying about 5% sodium hydroxide solution through an alkali solution tank J-1, recycling alkali solution after use through an alkali solution recycling tank J-2, connecting a discharge hole of a pretreatment tank P-1 with an anaerobic fermentation device, carrying out anaerobic fermentation on biomass after lignin removal by adopting an anaerobic fermentation tank R-1 in the anaerobic fermentation device of the embodiment to generate methane and carbon dioxide, arranging a drying tower D-1 at a gas outlet of the anaerobic fermentation tank R-1 to dry generated gas, connecting a gas outlet of the drying tower with a carbon dioxide separation tower S-1, sending separated and purified carbon dioxide into a carbon dioxide storage tank C-1, connecting a tail gas outlet of the carbon dioxide separation tower S-1 to a methane separation tower S-2, storing separated methane into the methane storage tank C-2, connecting an outlet of the methane storage tank C-2 with a microwave reactor R-2, reacting methane to generate acetylene and simultaneously generating a large amount of hydrogen, connecting an outlet of the microwave reactor R-2 with a hydrogen separation tower S-3 to separate hydrogen, sending the hydrogen into the hydrogen storage tank C-3, sending the gas after hydrogen removal into the trimerization reactor R-3, generating light aromatic hydrocarbon under the action of a catalyst, and connecting the hydrogen storage tank C-3 to a hydrogen storage tank C-4, and catalyzing the hydrogen storage tank C-4 to generate methanol.|[0043] The process of the method mainly comprises the following steps:|[0044] (1) Crushing biomass and preprocessing; biomass particles of about 0.5 cm are conveyed to a pretreatment tank P-1 by a screw feeder to be soaked for 24 hours, and 4mol/L sodium hydroxide solution is filled in the biomass particles to remove lignin.|[0045] (2) Anaerobic fermentation is carried out on the pretreated biomass particles to generate methane and carbon dioxide; filtering the pretreated biomass particles to perform solid-liquid separation, recycling alkali liquor, and transferring the solid to an anaerobic fermentation tank R-1 at 35 ℃ for fermentation for 3 days, wherein the stirring speed of a stirring paddle of the fermentation tank is set to 40rpm, and the pH value of the system is controlled to be 6.8-7.2.|[0046] (3) Drying, purifying and separating methane and carbon dioxide; and enabling gas-phase products generated in the anaerobic fermentation tank R-1 to enter a methane and carbon dioxide storage tank after passing through a drying tower and a separation tower respectively.|[0047] (4) Carrying out microwave reaction on methane to obtain acetylene, and carrying out trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon; introducing methane obtained by fermentation into a methane microwave conversion reactor at a flow rate of 30mL/min for conversion, wherein the conversion rate can reach 92%, and C 2 The yield of acetylene can reach 90 percent, the yield of acetylene can reach 88 percent, a large amount of hydrogen is produced at the same time, the hydrogen is purified by pressure swing adsorption and then is temporarily stored in a hydrogen storage tank C-3, the residual acetylene passes through an acetylene trimerization reactor, wherein the catalyst is a catalyst of molecular sieve or porous silicon dioxide loaded noble metals Ru, pd and the like, and the reaction space velocity is about 500h -1 The reaction temperature is 500 ℃, and light aromatic hydrocarbon can be obtained, in the reaction process, the conversion rate of acetylene can reach about 90 percent, and the selectivity of the light aromatic hydrocarbon can reach more than 65 percent.|[0048] CH 4 →C+2H 2|[0049] CO 2 +3H 2 →CH 3 OH+H 2 O|[0050] 3C 2 H 2 →C 6 H 6|[0051] Decomposing carbon dioxide and methane generated by anaerobic fermentation into hydrogen gas, and using H 2 :CO 2 =3:1, reaction space velocity of 5500h -1 Methanol can be produced under the action of 8Mpa at 210 ℃ in the presence of Zn-Zr catalyst. If abnormal conditions occur in the reaction process, CO can also be added by alkali liquor 2 Absorbing or discharging the combustible gas into the incineration system for power generation, reducing the risk as low as possible, and for this purpose the methane storage tank and the methane separation column are also provided with emergency pipes leading to the incineration device.|[0052] As for the selection of other reaction parameters, the person skilled in the art can determine, for example, that the pH value of the anaerobic fermentation system can be adjusted between 6.8 and 7.2 according to common general knowledge, and the details are omitted.|[0053] The foregoing is merely exemplary of the present application, and specific structures, characteristics, and proportions of reactants, etc. that are well known in the art are not described in detail herein. It should be noted that modifications and improvements can be made by those skilled in the art without departing from the spirit of the application, such as the selection of simple adjustment parameters within or near the specified parameters, which should also be considered as the scope of the application, which does not affect the effect of the practice of the application and the utility of the patent. The protection scope of the present application is subject to the content of the claims, and the description of the specific embodiments and the like in the specification can be used for explaining the content of the claims. (CN117046398)|TECHNICAL FIELD|[0001] The application belongs to the technical field of biomass treatment, and particularly relates to a process and equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwaves.|BACKGROUND ART|[0002] Light aromatic compounds (benzene, toluene, xylene and the like) are used as important basic chemical raw materials for various chemical products. Generally, the compounds are mainly derived from non-renewable petroleum resources, and a part of the compounds are derived from coal chemical processes, but China also has the characteristics of lean oil and less gas, so that development of an alternative light aromatic hydrocarbon process route has strong practical significance.|[0003] Renewable biomass resources can not only obtain light aromatic hydrocarbon through a series of thermocatalytic processes, but also realize the recycling and high value-added utilization of biomass, and are also considered as one of important ways for realizing carbon peak and carbon neutralization in the early days, so that the method accords with the development trend of the current society.|DISCLOSURE|Disclosure of Invention|[0004] The application aims to provide a biomass conversion process for solving the problem of low economic value of methane generated in the existing biomass anaerobic fermentation.|[0005] In order to solve the problems, the application provides a process for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwave, which comprises the following steps:|[0006] (1) Crushing biomass and preprocessing;|[0007] (2) Filtering the pretreated biomass particles, and performing anaerobic fermentation to generate methane and carbon dioxide;|[0008] (3) Drying, purifying and separating methane and carbon dioxide;|[0009] (4) Carrying out microwave reaction on methane to obtain acetylene, and carrying out trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon;|[0010] (5) And (3) carrying out a methanol synthesis reaction on the hydrogen generated in the step (4) and the carbon dioxide separated in the step (3) to obtain methanol.|[0011] The biomass is subjected to anaerobic fermentation to obtain methane, the methane can be converted into acetylene through microwaves, and then the acetylene can obtain light aromatic hydrocarbon compounds through a thermocatalytic process under the condition of a catalyst, so that the utilization value of the biomass is improved. In addition, a great amount of hydrogen is generated in the process of generating acetylene through methane microwave conversion, and a part of carbon dioxide is generated as a byproduct in the biomass anaerobic fermentation process besides a great amount of methane, and the part of carbon dioxide is combined with the hydrogen generated by methane decomposition to generate bulk chemicals of methanol in the presence of a catalyst, so that the methane generated by biomass anaerobic fermentation can be converted into light aromatic chemical products in the process, and the value of the light aromatic chemical products is improved; the byproduct carbon dioxide and hydrogen can be converted into bulk chemical methanol, and a new path is opened up for upgrading and comprehensive utilization of biomass.|[0012] Preferably, in order to facilitate the subsequent anaerobic fermentation of the biomass particles, the pretreatment in the step (1) comprises soaking the crushed biomass particles in NaOH solution for 24 hours to remove lignin better.|[0013] In the step (2), the temperature of the reaction system is maintained at 35 ℃ and the pH is maintained at 6.8-7.2 until the amount of generated gas is obviously reduced, and residues are removed and pretreated biomass particles are added again in order to improve the efficiency of anaerobic fermentation.|[0014] In a preferred scheme, in order to better purify the generated hydrogen, the subsequent methanol synthesis reaction is conveniently and smoothly carried out, and the hydrogen generated by pressure swing adsorption purification is carried out after the step (4).|[0015] In order to ensure efficient methanol synthesis, the methanol synthesis reaction in the step (5) adopts a Zn-Zr catalyst, wherein the reaction temperature is 210 ℃ and the pressure is 8Mpa.|[0016] The application also aims to provide equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwave, which comprises a pretreatment device, an anaerobic fermentation device, a methane microwave conversion device, an acetylene trimerization reaction device and a methanol synthesis reaction device which are sequentially arranged; wherein,|[0017] the pretreatment device is used for soaking biomass particles in alkali liquor and removing lignin;|[0018] the anaerobic fermentation device is used for carrying out anaerobic fermentation on biomass particles to generate methane and carbon dioxide;|[0019] the methane microwave conversion device is used for converting methane into acetylene;|[0020] the acetylene trimerization reaction device is used for converting acetylene into light aromatic hydrocarbon;|[0021] a methanol synthesis reaction device for preparing the hydrogen and the carbon dioxide into the methanol through the methanol synthesis reaction|[0022] As a preferable scheme, a drying tower, a carbon dioxide separation tower and a methane separation tower are further arranged behind the anaerobic fermentation device in sequence, and the carbon dioxide separation tower and the methane separation tower are respectively connected with a carbon dioxide storage tank and a methane storage tank.|[0023] As a preferable scheme, a gas outlet of the methane microwave conversion device is connected with a pressure swing adsorption device and a hydrogen storage tank.|[0024] Preferably, in order to avoid the risk of occurrence of abnormal conditions, the methane tank and the methane separation tower are further provided with emergency pipes leading to the incineration device.|[0025] The method is coupled with anaerobic fermentation, microwave conversion, acetylene trimerization and methanol synthesis processes, and directly converts biomass into light aromatic hydrocarbon compounds and combines with bulk chemicals methanol. The process can not only effectively solve the problem that light aromatic hydrocarbon is derived from renewable resources, but also coproduce and produce bulk chemicals methanol, plays a role in carbon fixation, and effectively solves the problems of recycling and upgrading of solid wastes. The main advantages are as follows:|[0026] (1) The application couples a plurality of processes together and is continuously operated to finally obtain the light aromatic hydrocarbon chemical raw material and bulk chemical methanol, thereby expanding the source of light aromatic hydrocarbon, converting non-renewable resources into renewable resources, fully utilizing carbon dioxide and playing a role of carbon fixation.|[0027] (2) The methane in the application generates a large amount of acetylene under the condition of microwave reaction, and the product not only can be used for synthesizing light aromatic compounds by trimerization, but also can be used for synthesizing other high-added-value chemicals according to different requirements, such as specific development of fine chemicals such as ethers, ketones, alcohols and the like with high added value, and has strong adjustable deformation.|[0028] (3) The application fully utilizes the carbon dioxide gas and a large amount of hydrogen generated by methane decomposition of byproducts in the reaction process, combines the characteristics of the reaction process, synthesizes a large amount of chemical methanol under the action of the catalyst, fully utilizes the byproducts, and forms a closed loop in the process from biomass to light aromatic hydrocarbon and methanol.|DRAWINGS DESCRIPTION|[0029] In order to more clearly illustrate embodiments of the present application or the prior art, the drawings that are required for the description of the embodiments or the prior art will be briefly described, and it is apparent that the drawings in the description below are some embodiments of the present application.|[0030] Fig. 1 shows an apparatus for producing light aromatic hydrocarbons and co-producing methanol by converting acetylene and trimerizing biomass by microwave in this example.|[0031] The drawings include: l-1, a screw feeder; j-1, alkali liquor tank 1; j-2, an alkali liquor recovery tank 1; p-1, a pretreatment tank; r-1 is an anaerobic fermentation tank; d-1, a drying tower; s-1, a carbon dioxide separation tower; s-2, a methane separation tower; s-3, a hydrogen separation tower; c-1, a carbon dioxide storage tank; c-2, a methane storage tank; c-3, a hydrogen storage tank; r-2 is a microwave reactor; r-3 is an acetylene trimerization reactor; r-4 is a methanol synthesis reactor.|INVENTION MODE|Detailed Description|[0032] The following examples are illustrative of the application and are not intended to limit the scope of the application. The specific techniques or conditions are not identified in the examples and are described in the literature in this field or are carried out in accordance with the product specifications.|[0033] In the description of the present application, unless otherwise indicated, the terms "upper," "lower," and the like refer to an orientation or state relationship based on that shown in the drawings, for convenience of description and simplicity of description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus should not be construed as limiting the application.|[0034] In the following examples, the equipment and the like used were conventional products available for purchase by a regular channel manufacturer, without specifying the manufacturer. The methods are conventional methods unless otherwise specified, and the starting materials are commercially available from the public sources unless otherwise specified.|[0035] Example 1|[0036] As shown in fig. 1, the embodiment provides a process and equipment for preparing light aromatic hydrocarbon and co-producing methanol by converting acetylene and trimerizing biomass by microwave, wherein the equipment comprises a pretreatment device, an anaerobic fermentation device, a methane microwave conversion device, an acetylene trimerization reaction device and a methanol synthesis reaction device which are sequentially arranged; wherein,|[0037] the pretreatment device is used for soaking biomass particles in alkali liquor and removing lignin;|[0038] the anaerobic fermentation device is used for carrying out anaerobic fermentation on biomass particles to generate methane and carbon dioxide;|[0039] the methane microwave conversion device is used for converting methane into acetylene;|[0040] the acetylene trimerization reaction device is used for converting acetylene into light aromatic hydrocarbon;|[0041] the methanol synthesis reaction device is used for preparing the methanol from the hydrogen and the carbon dioxide through the methanol synthesis reaction.|[0042] Specifically, the pretreatment device adopts a pretreatment tank P-1, and crushed biomass is supplied to the pretreatment tank P-1 through a screw feeder L-1; the method comprises the steps of supplying about 5% sodium hydroxide solution through an alkali solution tank J-1, recycling alkali solution after use through an alkali solution recycling tank J-2, connecting a discharge hole of a pretreatment tank P-1 with an anaerobic fermentation device, carrying out anaerobic fermentation on biomass after lignin removal by adopting an anaerobic fermentation tank R-1 in the anaerobic fermentation device of the embodiment to generate methane and carbon dioxide, arranging a drying tower D-1 at a gas outlet of the anaerobic fermentation tank R-1 to dry generated gas, connecting a gas outlet of the drying tower with a carbon dioxide separation tower S-1, sending separated and purified carbon dioxide into a carbon dioxide storage tank C-1, connecting a tail gas outlet of the carbon dioxide separation tower S-1 to a methane separation tower S-2, storing separated methane into the methane storage tank C-2, connecting an outlet of the methane storage tank C-2 with a microwave reactor R-2, reacting methane to generate acetylene and simultaneously generating a large amount of hydrogen, connecting an outlet of the microwave reactor R-2 with a hydrogen separation tower S-3 to separate hydrogen, sending the hydrogen into the hydrogen storage tank C-3, sending the gas after hydrogen removal into the trimerization reactor R-3, generating light aromatic hydrocarbon under the action of a catalyst, and connecting the hydrogen storage tank C-3 to a hydrogen storage tank C-4, and catalyzing the hydrogen storage tank C-4 to generate methanol.|[0043] The process of the method mainly comprises the following steps:|[0044] (1) Crushing biomass and preprocessing; biomass particles of about 0.5 cm are conveyed to a pretreatment tank P-1 by a screw feeder to be soaked for 24 hours, and 4mol/L sodium hydroxide solution is filled in the biomass particles to remove lignin.|[0045] (2) Anaerobic fermentation is carried out on the pretreated biomass particles to generate methane and carbon dioxide; filtering the pretreated biomass particles to perform solid-liquid separation, recycling alkali liquor, and transferring the solid to an anaerobic fermentation tank R-1 at 35 ℃ for fermentation for 3 days, wherein the stirring speed of a stirring paddle of the fermentation tank is set to 40rpm, and the pH value of the system is controlled to be 6.8-7.2.|[0046] (3) Drying, purifying and separating methane and carbon dioxide; and enabling gas-phase products generated in the anaerobic fermentation tank R-1 to enter a methane and carbon dioxide storage tank after passing through a drying tower and a separation tower respectively.|[0047] (4) Carrying out microwave reaction on methane to obtain acetylene, and carrying out trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon; introducing methane obtained by fermentation into a methane microwave conversion reactor at a flow rate of 30mL/min for conversion, wherein the conversion rate can reach 92%, and C 2 The yield of acetylene can reach 90 percent, the yield of acetylene can reach 88 percent, a large amount of hydrogen is produced at the same time, the hydrogen is purified by pressure swing adsorption and then is temporarily stored in a hydrogen storage tank C-3, the residual acetylene passes through an acetylene trimerization reactor, wherein the catalyst is a catalyst of molecular sieve or porous silicon dioxide loaded noble metals Ru, pd and the like, and the reaction space velocity is about 500h -1 The reaction temperature is 500 ℃, and light aromatic hydrocarbon can be obtained, in the reaction process, the conversion rate of acetylene can reach about 90 percent, and the selectivity of the light aromatic hydrocarbon can reach more than 65 percent.|[0048] CH 4 →C+2H 2|[0049] CO 2 +3H 2 →CH 3 OH+H 2 O|[0050] 3C 2 H 2 →C 6 H 6|[0051] Decomposing carbon dioxide and methane generated by anaerobic fermentation into hydrogen gas, and using H 2 :CO 2 =3:1, reaction space velocity of 5500h -1 Methanol can be produced under the action of 8Mpa at 210 ℃ in the presence of Zn-Zr catalyst. If abnormal conditions occur in the reaction process, CO can also be added by alkali liquor 2 Absorbing or discharging the combustible gas into the incineration system for power generation, reducing the risk as low as possible, and for this purpose the methane storage tank and the methane separation column are also provided with emergency pipes leading to the incineration device.|[0052] As for the selection of other reaction parameters, the person skilled in the art can determine, for example, that the pH value of the anaerobic fermentation system can be adjusted between 6.8 and 7.2 according to common general knowledge, and the details are omitted.|[0053] The foregoing is merely exemplary of the present application, and specific structures, characteristics, and proportions of reactants, etc. that are well known in the art are not described in detail herein. It should be noted that modifications and improvements can be made by those skilled in the art without departing from the spirit of the application, such as the selection of simple adjustment parameters within or near the specified parameters, which should also be considered as the scope of the application, which does not affect the effect of the practice of the application and the utility of the patent. The protection scope of the present application is subject to the content of the claims, and the description of the specific embodiments and the like in the specification can be used for explaining the content of the claims. Family Number|(107276761)|107276761|Abstract|(CN117046398 A)|The invention belongs to the technical field of biomass treatment , and particularly relates to a process for preparing light aromatic hydrocarbon and co - producing methanol through biomass microwave conversion acetylene trimerization , which comprises the following steps : ( 1 ) crushing and pretreating biomass ; ( 2 ) carrying out anaerobic fermentation on the pretreated biomass particles to generate methane and carbon dioxide ; ( 3 ) drying , purifying and separating methane and carbon dioxide ; ( 4 ) performing microwave reaction on methane to obtain acetylene , and performing trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon ; and performing methanol synthesis reaction on the hydrogen generated in the step ( 4 ) and the carbon dioxide separated in the step ( 3 ) to obtain methanol . According to the process , anaerobic fermentation , microwave conversion , acetylene trimerization and methanol synthesis processes are coupled , biomass is directly converted into light aromatic hydrocarbon compounds , a bulk chemical methanol is co - produced , a carbon sequestration effect is achieved , and the problems of solid waste recycling and quality improvement are effectively solved . |CPC codes|(CN117046398 A)|B01J - 008/00 |B01J - 019/00 |B01J - 019/12/6 |B01J - 2219/00033 |IPC codes|(CN117046398 A)|B01J - 008/00 |B01J - 019/00 |B01J - 019/12 | Biotechnology|Chemical engineering|Food chemistry B01J-008/00|B01J-019/00|B01J-019/12/6|B01J-2219/00033|C12F-003/02|C12M-021/04|C12M-023/36|C12M-045/06|C12M-047/12|C12M-047/14|C12P-005/02/3 B01J-008/00|B01J-019/00|B01J-019/12/6|B01J-2219/00033|C12F-003/02|C12M-021/04|C12M-023/36|C12M-045/06|C12M-047/12|C12M-047/14|C12P-005/02/3 B01J-008/00|B01J-019/00|B01J-019/12|C12F-003/02|C12M-001/00|C12M-001/107|C12P-005/02 B01J-008/00|B01J-019/00|B01J-019/12|C12F-003/02|C12M-001/00|C12M-001/107|C12P-005/02 CN116477607|CN115368198|CN107686744|CN107570204 CN116477607 105849107 WHO=Examiner SELF=Y CAT=Y|CN115368198 102673079 WHO=Examiner SELF=Y CAT=Y|CN107686744 78768983 WHO=Examiner SELF=N CAT=Y|CN107570204 78470945 WHO=Examiner SELF=N CAT=A CN107570204; CN107686744; CN115368198; CN116477607 PENDING (CN117046398)|PENDING ALIVE (CN117046398)|ALIVE (CN117046398)|LEGAL DETAILS FOR CN117046398|Actual or expected expiration date=2043-08-17|Legal state=ALIVE|Status=PENDING|Event publication date=2023-08-17|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202311039076|Application date=2023-08-17|Standardized application number=2023CN-1039076|Event publication date=2023-11-14|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN117046398|Publication stage code=A|Publication date=2023-11-14|Standardized publication number=CN117046398|Event publication date=2023-11-14|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2023-12-01|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN117046398)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRwnorn+1PGFlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000070217987&ekey=2177&xpn=CN117046398&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=L8ZoB0GML9rGrpPachSyZpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN117046398)|CN (CN117046398)|NAME=CECEP ENG TECH RES INST CO LTD , COUNTRY=CN (CN117046398)|NAME=ZHU DONG;CHONG QING CUI ZHI BANG CHENG ZHUAN LI DAI LI SHI WU SUO (PU TONG HE HUO) , REG=50231 (CN117046398)|NAME=LI QINGYUAN|NAME=XU SHIPEI|NAME=LU JIANWEN|NAME=WANG CHAO 0 1 Titre: (CN117046398)|Process and equipment for preparing light aromatic hydrocarbon and co-producing methanol through acetylene trimerization through biomass microwave conversion Résumé: (CN117046398)|The invention belongs to the technical field of biomass treatment, and particularly relates to a process for preparing light aromatic hydrocarbon and co-producing methanol through biomass microwave conversion acetylene trimerization, which comprises the following steps: (1) crushing and pretreating biomass; (2) carrying out anaerobic fermentation on the pretreated biomass particles to generate methane and carbon dioxide; (3) drying, purifying and separating methane and carbon dioxide; (4) performing microwave reaction on methane to obtain acetylene, and performing trimerization reaction on the obtained acetylene to obtain light aromatic hydrocarbon; and performing methanol synthesis reaction on the hydrogen generated in the step (4) and the carbon dioxide separated in the step (3) to obtain methanol. According to the process, anaerobic fermentation, microwave conversion, acetylene trimerization and methanol synthesis processes are coupled, biomass is directly converted into light aromatic hydrocarbon compounds, a bulk chemical methanol is co-produced, a carbon sequestration effect is achieved, and the problems of solid waste recycling and quality improvement are effectively solved. 119 Abstract gpt-4o-mini no The article focuses on biomass conversion and methanol production, not on accelerated weathering or CO₂ capture through mineral alteration.
123 IN202441053277 IN202441053277 IN202441053277 110856270 IN202441053277 A 2024-07-26 [IN202441053277] 2024-07-12 2024-07-12 2024-07-26 (IN202441053277)|2044-07-12 (IN202441053277)|Synthesis of activated carbon for the removal of heavy metals from the aqueous solution (IN202441053277)|This study explores the preparation and characterization of activated carbon derived from “Azadirachta indica” wood, a widely available waste material in Tamil Nadu, India. With increasing industrialization, the management of heavy metal contamination has become critical. This research aims to utilize “Azadirachta indica” wood as a sustainable and cost-effective adsorbent for the removal of copper sulfate (CuSO4) from aqueous solutions. The methodology involved the collection of “Azadirachta indica” wood, which was subsequently crushed and thoroughly washed to eliminate dust and impurities. The wood was dried using sunlight and a hot air oven, then ground into a fine powder. For the activation process, the wood was treated with potassium hydroxide (KOH) and subjected to high temperatures (2600°C) in a furnace for a specified duration. Following activation, the product was washed multiple times with hot water to remove free acids and moisture, resulting in a brown-colored activated carbon ready for characterization. Characterization techniques employed included Fourier Transform Infrared Spectroscopy (FTIR) and Scanning Electron Microscopy (SEM). FTIR analysis revealed significant absorption peaks corresponding to functional groups associated with activated carbon, such as O-H stretching and C=O vibrations. SEM images displayed a porous structure with irregular particles, highlighting the effective surface area available for adsorption. The effectiveness of the activated carbon as an adsorbent was evaluated through a series of batch adsorption experiments with varying concentrations of CuSO4. The results indicated a maximum removal efficiency of 96% when 0.5 grams of activated carbon were used in a 25 mL solution of CuSO4. This demonstrates the high adsorption capacity of the activated carbon produced from “Azadirachtaindica”wood, underscoring its potential for treating industrial effluents. Furthermore, the study examined the influence of various operational parameters such as dosage, pH, and contact time on the adsorption efficiency. The optimal conditions were determined, with the results suggesting that the order of significance for the adsorption process is as follows: adsorption time > dosage > pH > temperature. This information can guide practical applications in effluent treatment systems. In conclusion, this research highlights the viability of utilizing “Azadirachta indica” wood as an effective and low-cost adsorbent for heavy metal removal. The findings contribute to environmental sustainability by promoting the use of agricultural waste in waste management processes. Future studies may focus on scaling up this process and exploring other waste materials for activated carbon production, further enhancing the feasibility of sustainable adsorbents in industrial applications. Keywords: Adsorption, azadirachta indica wood powder, cuso4, Freundlich and Langmuir Isothermetting a raw material as a powder form. Anbu A|Gowrishankar R|Gunasekaran Gnanapragasam|Mappilaimeeran S|Premkumar G|Saravanan S|Thaarun S (IN202441053277)|Gunasekaran Gnanapragasam|Anbu A|Gowrishankar R|Premkumar G|Thaarun S|Mappilaimeeran S|Saravanan S Gunasekaran Gnanapragasam|Anbu A|Gowrishankar R|Premkumar G|Thaarun S|Mappilaimeeran S|Saravanan S (IN202441053277)|Gunasekaran Gnanapragasam|Anbu A|Gowrishankar R|Premkumar G|Thaarun S|Mappilaimeeran S|Saravanan S (IN202441053277)|It is useful in medicine, but utilization of Azadirachta indica wood using various treatments can be used as a low cost adsorbent instead of high cost adsorbent.|It shows better results than optical microscopy because of its high and better resolution and enhanced depth of field.|Performing activation and carbonization simultaneously during the chemical activation process at lower temperature results in having better porous structures of AC, even though, concern about environmental protection may limit the use of chemical agents for activation.|The potentiality of Neem has also been widely studied by different researchers for solving most of the problems related to agriculture, environmental pollution public health, population control.|The presence of heavy metals water has become a major problem in today's world due to its direct effect on all living organisms especially on human beings.| (IN202441053277)|1. The scope of the study was to investigate the synthesis of activated carbon from Azadirachta indica for the removal of heavy metals from aqueous solution effluents using activated carbon as an adsorbent. 1: Azadirachta indica wood collected from Erode district was processed by washing it five times with tap water and three times with distilled water to remove dust and impurities. It was then dried in sunlight and a hot air oven for two hours, and finally ground into powder form using a ball mill.|2. Using 25 mL of distilled water and 25 mL of heavy metal solution, along with 0.5 grams of activated carbon, resulted in 48 mL of pure water, constituting 96% of the total solution.|3. A solution comprising 25 mL of distilled water, 20 mL of heavy metal solution, and 1.0 gram of activated carbon yielded 39 mL of pure water, making up 78% of the total solution.|4. With 25 mL of distilled water, 15 mL of heavy metal solution, and 1.5 grams of activated carbon, the outcome was 33 mL of pure water, which accounted for 66% of the total solution.|5. The mixture of 25 mL of distilled water, 10 mL of heavy metal solution, and 2.0 grams of activated carbon produced 32 mL of pure water, representing 64% of the total solution.|6. Using 25 mL of distilled water, 5 mL of heavy metal solution, and 2.5 grams of activated carbon resulted in 28 mL of pure water, comprising 56% of the total solution.| (IN202441053277)|This study explores the preparation and characterization of activated carbon derived from "Azadirachta indica" wood, a widely available waste material in Tamil Nadu, India. With increasing industrialization, the management of heavy metal contamination has become critical.| (IN202441053277)|ACTIVATED CARBON(100,65)|AZADIRACHTA INDICA(100,20)|HEAVY METAL(100,14)|DISTILLED WATER(100,8)|HEAVY METAL REMOVAL(100,6)|ADSORBENT(100,5)|AQUEOUS SOLUTION(100,5)|HEAVY METAL SOLUTION(100,5)|PURE WATER(100,5)|TOTAL SOLUTION(100,5)|ACTIVATED CARBON SYNTHESIS(100,2)|OUTCOME(100,1)|SOLUTION WATER EFFLUENT(100,1)|STUDY SCOPE(100,1)|SUSTAINABLE ADSORBENT FEASIBILITY(100,1)|AZADIRACHTA INDICA WOOD(68,11)|AZADIRACHTA INDICA WOOD POWDER(60,1)|INDUSTRIALIZATION(55,1)|BATCH ADSORPTION(48,1)|WOOD(47,7)|ENVIRONMENTAL POLLUTION PUBLIC HEALTH(41,1)|ACTIVATED CARBON CHARACTERIZATION(38,1)|IRREGULAR PARTICLE(37,1)|OPERATING PARAMETER(37,1)|IMPURITY(34,3)|SUNLIGHT(34,3)|CARBONIZATION(33,1)|DEPTH ENHANCEMENT(32,1)|INDUSTRIAL EFFLUENT TREATMENT(32,1)|AGRICULTURE(30,1)|LIVING ORGANISM(29,1)|DISTRICT(28,2)|CUSO4 SOLUTION(28,1)|DUST(27,2)|FINE POWDER(26,1)|ENVIRONMENTAL SUSTAINABILITY(25,1)|VIABILITY(25,1)|ENHANCING(23,1)|HEAVY METAL CONTAMINATION MANAGEMENT(23,1)|KEYWORD(23,1)|PUBLIC HEALTH(23,1)|DOSAGE(22,3)|ENVIRONMENTAL POLLUTION(21,2)|ENVIRONMENTAL PROTECTION(21,1)|ACTIVATION(20,3)|COPPER SULFATE REMOVAL(20,1)|OPTICAL MICROSCOPY(20,1)|SCORING(20,1)|MAXIMUM REMOVAL(19,1)|SCALING(19,1)|BALL MILL(17,3)|ACTIVATED CARBON READY(17,1)|ADSORPTION(16,1)|FUTURE STUDY(16,1)|FOURIER TRANSFORM INFRARED SPECTROSCOPY(15,4)|POROUS STRUCTURE(15,1)|LOW COST ADSORBENT(14,2)|ACTIVATED CARBON PRODUCTION(14,1)|COST EFFECTIVE ADSORBENT(14,1)|O H STRETCHING(14,1)|STEAM PYROLYSIS(13,3)|POTASSIUM HYDROXIDE(13,2)|HEAVY METAL CONTAMINATION(12,1)|SCANNING ELECTRON MICROSCOPY(11,11)|HOT WATER(11,3)|TAP WATER(11,2)|ADSORBENT MACROPORE(11,1)|CHEMICAL AGENT(11,1)|COPPER DOPED ZNO NPS(11,1)|FIELD ENHANCED DEPTH(11,1)|WASTE MANAGEMENT(11,1)|ZINC BIOSORPTION EQUILIBRIUM(11,1)|HAZELNUT SHELL(10,2)|BIOSORPTION KINETICS(10,1)|HEAVY METAL WATER(10,1)|ORGANIC BIOMASS THERMOCHEMICAL CONVERSION(10,1)|REFRIGERATOR DEODORIZER(10,1)|REMOVING HEAVY METAL(10,1)|TRIHYDROXIDOOXIDO PHOSPHORUS(10,1)|CUSO REMOVAL(9,3)|ALMOND SHELL(9,2)|NATURAL ADSORBENT(9,2)|SILICA CRUCIBLE(9,2)|HOT AIR OVEN(8,4)|WASTE MATERIAL(8,3)|ALDEHYDE BENDING VIBRATION(8,1)|APRICOT STONE(8,1)|BIOMASS MAJOR DECOMPOSITION(8,1)|COCO NUTSHELL(8,1)|IRREGULAR MACROPORE(8,1)|POPULATION CONTROL(8,1)|SWEDISH CHEMIST(8,1)|TEMPERATURE RESULT(8,1)|ADSORPTION TIME(7,2)|FUNCTIONAL GROUP(7,2)|VOLATILE MATTER(7,2)|ACTIVATED BLACK COLORED ADSORBENT(7,1)|AGRICULTURAL WASTE BIOMASS(7,1)|BAGASSE FLY ASH(7,1)|CASSAVA PEEL(7,1)|CHERRY STONE(7,1)|FERTILIZER PLANT(7,1)|FRUIT STONE(7,1)|GROUNDNUT SHELL(7,1)|HIGH COST ADSORBENT(7,1)|HUGE MOMENTUM(7,1)|JUJUBE SEED(7,1)|MANGOSTEEN SHELL(7,1)|NEEM LEAVE POWDER(7,1)|OLIVE STONE(7,1)|PAPAYA SEED(7,1)|PHENOL ADSORPTION(7,1)|PREPARED BROWN COLORED ADSORBENT(7,1)|TREE LEAVE(7,1)|UNEVEN TOPOGRAPHY(7,1)|ZN CALCINATION(7,1)|ZNO STRETCHING FREQUENCY(7,1)|RICE HUSK(6,3)|ASH CONTENT(6,2)|WASTE MATERIAL AVAILABILITY(6,2)|ADSORPTIVE ABILITY(6,1)|ADSORPTIVE CAPACITY(6,1)|AGRICULTURAL RESIDUE PROXIMATE ANALYSIS(6,1)|BIOCHEMICAL INDUSTRY(6,1)|CHAR RESIDUE(6,1)|CONTACTOR LABORATORY PLASTIC COLUMN(6,1)|DIRECT EFFECT(6,1)|DUST PARTICLE(6,1)|FEDERAL LAW DIRECTING REMOVAL(6,1)|FIX BED PYROLYSIS(6,1)|FOCUSED ELECTRON(6,1)|INDUSTRIAL EFFLUENT ADSORPTION CAPACITY(6,1)|LABORATORY SETUP(6,1)|OLIVE SEED(6,1)|OPTIMUM POLLUTANT REMOVAL(6,1)|PALM SHELL(6,1)|PEACH WASTE(6,1)|PERSONAL TOOL PROTECTION(6,1)|PROJECTED DEMAND(6,1)|SOLUBLE IMPURITY(6,1)|TOBACCO STEM(6,1)|TROPICAL WOOD WASTE(6,1)|ULTIMATE ANALYSIS(6,1)|VITAL ROLE(6,1)|WELL STRUCTURE POROSITY(6,1)|BANANA PEEL(5,2)|COLLOIDAL SOLUTION(5,2)|ELECTROLYSIS(5,2)|SPECIMEN(5,2)|TURBIDITY(5,2)|WORLD WAR(5,2)|ABSORPTION PEAK INTENSITY(5,1)|ACTIVATION REACTOR(5,1)|ANALYTICAL EQUIPMENT(5,1)|BOD RATIO(5,1)|BURNT CARBON(5,1)|CAVITY EXPANSION(5,1)|CHAR PRODUCTION(5,1)|CHAR YIELD(5,1)|DECOLORIZE(5,1)|IMPREGNATION RATIO(5,1)|INDUSTRIAL APPLICATION(5,1)|NERVE GAS TRAPPING(5,1)|PALE GREEN(5,1)|PERMISSIBLE LIMIT(5,1)|PRETREATMENT(5,1)|RAISED ASH(5,1)|RECTANGULAR RASTER(5,1)|SCAN COIL(5,1)|SUGAR REFINING INDUSTRY(5,1)|SYNTHESIZED OXIDE(5,1)|VIBRATION BAND(5,1)|ZNO STANDARD PEAK(5,1)|CO2(4,3)|COCONUT SHELL(4,3)|COD(4,3)|TSS(4,3)|ABDOMINAL PAIN(3,1)|ACIDIC GAS ADSORPTION(3,1)|ACTIVATED CARBON 5GM(3,1)|ACTIVATION GAS(3,1)|ATMOSPHERIC AIR CONTAMINANT CLEANING(3,1)|AUTOMATIC ADJUSTMENT(3,1)|BASIC GAS ADSORPTION(3,1)|CARBON FLY ASH(3,1)|CARBONIZATION TEMPERATURE(3,1)|CENTRIFUGE(3,1)|CENTURY(3,1)|CHEMICAL ENGINEERING LABORATORY(3,1)|CHEMISORPTION(3,1)|CONTACT TIME(3,1)|COSMETICS(3,1)| (IN202441053277)|1. The scope of the study was to investigate the synthesis of activated carbon from Azadirachta indica for the removal of heavy metals from aqueous solution effluents using activated carbon as an adsorbent. 1: Azadirachta indica wood collected from Erode district was processed by washing it five times with tap water and three times with distilled water to remove dust and impurities. It was then dried in sunlight and a hot air oven for two hours, and finally ground into powder form using a ball mill.|2. Using 25 mL of distilled water and 25 mL of heavy metal solution, along with 0.5 grams of activated carbon, resulted in 48 mL of pure water, constituting 96% of the total solution.|3. A solution comprising 25 mL of distilled water, 20 mL of heavy metal solution, and 1.0 gram of activated carbon yielded 39 mL of pure water, making up 78% of the total solution.|4. With 25 mL of distilled water, 15 mL of heavy metal solution, and 1.5 grams of activated carbon, the outcome was 33 mL of pure water, which accounted for 66% of the total solution.|5. The mixture of 25 mL of distilled water, 10 mL of heavy metal solution, and 2.0 grams of activated carbon produced 32 mL of pure water, representing 64% of the total solution.|6. Using 25 mL of distilled water, 5 mL of heavy metal solution, and 2.5 grams of activated carbon resulted in 28 mL of pure water, comprising 56% of the total solution. (IN202441053277)|The Azadirachta indica wood were collected at hometown, Erode district and it was crushed into small pieces, and then washed repeatedly with tap water for 5 times and distilled water for 3 times because of removing unwanted dust particles and impurities in the leaves. Then it was dried in sunlight as well as in hot air oven for 2 hours and then grinded in ball mill for getting a raw material as a powder form.|PREPARATION OF ACTIVATED CARBON|Initially Azadirachta indica woods were washed repeatedly by using distilled water to remove moisture and soluble impurities. Then Azadirachta indica woods kept in oven at 900C, for 2-3 hrs till leaves turn pale Green. Then crushed and screen by 10-15 and kept in oven 20-25 minute. After drying powder was mixed with KOH in silica crucible and kept in furnace at 2600C for 4 hrs The heating period depend on atmospheric temperature then solution was cooled & repeatedly washed using hot water to remove free acid and moisture, total 11 washing taken and kept it in oven for 20-25 minute the prepared brown colored adsorbent kept in bottle for further Characterization process use.|About 20 gm sample and 10ml KOH taken in silica crucible and kept in furnace. The furnace is initially at normal room temperature then furnace set at 2600C. Heating was carried out for 4 Hour. Then sample was removed and cool. After cooling the sample was repeatedly washed for 11 times using hot water to remove free acid and moisture. Then sample kept in oven for 20-25 minute and the activated black colored adsorbent stored in bottle for further Characterization process use.|MATERIALS|MATERIAL USED|- Water|- Clay|- Azadirachta indica wood|CHEMICAL USED|- Ethanol|- KOH|EQUIPMENT USED|- Ball mill|- Hot air oven|- Muffle furnace|- Magnetic stirrer|- Centrifuge|ANALYTIC EQUIPMENT USED|- FT-IR|- SEM|Types of Adsorption|There are two types of Adsorption a. Physical Adsorption or Physiosorption b. Chemical Adsorption or Chemisorption.|The presence of heavy metals water has become a major problem in today’s world due to its direct effect on all living organisms especially on human beings. If these present in quantities above a certain permissible limit, they can cause various short and long-term hazardous and harmful effects, such as shortness of breath and lungs, coughing, and wheezing leading to gastrointestinal effects, such as abdominal pain, vomiting, hemorrhage, and neurological effects.|Waste streams containing various heavy metals such as Pb, Cd, Cr, Cu, Zn, Ni are often encountered in various chemical and biochemical industries. Activated carbon has been also used as a natural.|Adsorbent for the removal of industrial effluent, but it is readily soluble under extreme pH conditions and also not cost effective. Other alternative materials such as Neem leaves, papaya seeds, rice husk and banana peel, carbon fly ash, cork waste, bagasse fly ash, groundnut shell, coconut have also been investigated.|These materials are waste products from industries and act as natural adsorbents. Under optimum conditions, they can exhibit up to 99%removal of heavy metal. These adsorbents are show high adsorption efficiency, easily available, economic and thus are more effective in the removal of heavy metals. Among all the natural adsorbents the Azadirachta Indica (neem) leaves has high potential to remove the heavy metals from effluent.|In India, Azadirachta indica (neem) is a tree which is commonly seen is all where India, the leaves of this tree is burnt and the burnt carbon can be utilized for the treatment and purification of water at a low cost without heavy operation. Heavy metal has been removed by neem leaves powder.|Some of the study reports the biosorption kinetics and the biosorption equilibrium of Zinc by Neem leaves and stem bark powder. Neem bark powder (NBP) has been used as an adsorbent for the removal of heavy metals from aqueous solutions.|The potentiality of Neem has also been widely studied by different researchers for solving most of the problems related to agriculture, environmental pollution public health, population control.|Hence in this present study, the Azadirachta indica (Neem) leaf powder is studied for his adsorptive capacity to remove metals from aqueous solution|ACTIVATED CARBON|The origin of activated carbon (AC) is associated with Ancient Egypt (1500 BC), whereby the Egyptians make use of its adsorbent characteristics for water purifications and medicinal purposes. During the last few years, adsorption of gases on charcoal has been reported by a Swedish chemist, Kar Wilhelm. Within recent decades, the AC was used in industries as a decolorizing agent. However, the potential use of AC was actually capitalized during the First World War, where by AC was used in gas mask against toxic gases. Respiratory protective devices were developed as personal protective tools against the use of toxic gases during wars. Hence, granular activated carbon (GAC) has found application during the first World War and still been used nowadays.|During the beginning of 20th century, the first AC production plant was commissioned in Germany purposely for a sugar refining industry. Lately, some of the plants emerged to produce AC for wastewater treatment processes. Recently, the AC is abundantly utilized as an air purifier in atmospheric air contaminant cleaning, color removal of industrial and automobile exhaust, food and pharmaceutical products also used as refrigerator deodorizers and in advanced applications such as nuclear plants. In the late 1930’s undoubtedly, AC gained huge momentum and popularity in industrial sectors, for both gaseous and aqueous phase applications. In fact, various new carbon production processes were developed to meet the continuous increasing industrial needs.|Within the period of 1939 to 1945, a considerable advancement took place whereby several chemically saturated carbon were produced for war and nerve gases trapping. As of 2014, the estimated amount of AC was assumed to be about 1.1 million metric tons from AC industries with a 10% increase in the projected demand for fresh AC. there will be an expected increase in demand for AC in the United States of America (USA) due to the new federal laws directing removal of heavy metals from coal-fed power plants|PYROLYSIS PROCESS|Thermo chemical conversion of organic biomass into gaseous or/and liquid fuels at extremely high temperature in the absence of halogen (mainly oxygen) is termed as pyrolysis. Pyrolysis is a simultaneous process that changes both the chemical composition and physical phase of materials and is irreversible. Pyrolysis process is mostly observed when materials are exposed to higher temperatures. Some features of pyrolysis such as temperature has the most significant effect and then followed by retention time, heating rate and nitrogen flow rate. Normally, when the reaction temperature increased, causes reduction in both AC and char production, while at the same time increasing the pyrolysis temperature leads to a drop off of solid yield and an increase in both gases and liquid percentages yield. On the other hand, raising the temperature leads to raised ash and AC percentage, whereas the volatile matter gets reduced. Therefore, AC with greater quality is obtained at a higher temperature. Moreover, increasing the temperature that eventually decreases char yield could also be because of major decomposition of biomass at elevated temperatures or in the course of secondary decomposition of char residues. At the same time, higher temperatures at which secondary decomposition occurs could lead to getting some gaseous products that are non-condensable and ultimately increasing gas yield. Presents laboratory setup for the activated reactor and fixed-bed pyrolysis.|PHYSICAL ACTIVATION PROCESS|Physical activation is a two-step process. Carbonization of carbonaceous materials comes first, then activation of the resulting char at high temperatures in the presence of CO2, steam, air or three mixtures serving as oxidizing gases.|The CO2 is usually used as activation gas being easy to handle, clean and possesses a slow reaction rate at a temperature process. A temperature range of 400°C and 850°C was found to be the carbonization temperature, though it may sometimes reach up to 1000°C while activation temperature between 600°C and 900°C.|CHEMICAL ACTIVATION PROCESS|In the chemical activation process, involves multiple two steps occurring simultaneously, with the chemical activating agents mixing with the precursor, as oxidants and dehydrates. Performing activation and carbonization simultaneously during the chemical activation process at lower temperature results in having better porous structures of AC, even though, concern about environmental protection may limit the use of chemical agents for activation. Moreover, some chemicals that are widely used as activating agents are zinc chloride (ZnCl2), potassium hydroxide (KOH), trihydroxidooxido phosphorus, phosphoric acid (H3PO4) and potassium carbonate (K2CO3). Whereas the agricultural wastes that are being reduced with the earlier mentioned chemicals consist of; olive seed, apricot stones, macadamia, pecan-shells, peanut-hulls, nut- shells, almond shells, corn-cob, hazelnut shells, rice husks, rice straw and Cassava peel.|STEAM PYROLYSIS|In this process, the raw agricultural waste materials are either heated at a temperature range of 500–700°C under a flow of pure steam or heated at a higher temperature range of 700– 800°C under a flowing steam. Steam pyrolysis has been widely studied and successfully applied on various types of agricultural waste biomass such as rice husk, jujube seed, sawdust, tropical wood waste, palm shells, durian peel, corn cobs, coconut shells, tobacco stems, hazelnut shell, banana peels, mangosteen shells, etc.|However, the AC produced by steam pyrolysis was generally reported to be less effective, with an exception of those produced from cherry stones, apricot and almond shell. the ultimate and proximate analysis of agricultural residues as they are generated in large quantity worldwide.|FACTORS AFFECTING AC PRODUCTION:|RAW MATERIALS|Most organic substances with high carbon content are potential raw materials for AC production. To produce a porous carbon structure, the under listed factors can be considered.|- High carbon content|- Low inorganic content (i.e. low ash)|- Potential extent of activation|- Low degradation upon storage|- High density and sufficient volatile content|- Stability of supply in the countries|- Inexpensive materials.|Lignocelluloses materials were generally accepted as precursor for AC production and constitute about 45% of the total raw materials used. The characteristics of some raw materials used in the AC production. To produce AC with low ash content, it is important to get materials with low inorganic content. Full control of the manufacturing process requires a moderately high volatile content. Coconut shell and fruit stones are the most commonly raw materials. This might be because of their hardness, volatile content, and relatively high density, and content, which make them most prepared for hard GAC production. Moreover, other materials for example coconutshell, olive stones and peach waste are commercially utilized for micro-porous AC production and as well find usage for a variety of applications.|TEMPERATURE|In the AC production, the activation temperature plays a vital role in affecting the characteristic of the AC produced. As for commercial purposes AC, it is normally carried out in a mixture of steam and CO2 at a temperature above 800°C. In recent times, researchers have been up-and-doing to optimize final activation temperature in order to reduce cost and period of AC production. Several studies have been reported which indicated that activation temperature has great influence surface area and production yield of AC. The activation temperature is between 200 to 1100°C. However, a temperature range of 400 to 500°C was reported by previous researchers to be considered regardless of time taken and the impregnation ratio for a variety of raw materials. Therefore, increasing activation temperature always results in the reduction of AC yield during production, which at the same time results in increasing the volume of volatile substances released. Generally, it is inappropriate to prepare AC at a temperature above 800°C.|This goes along with an increase of fixed carbon and ash content, which may be ascribed to the removal of volatile matter in the material during carbonization process. Thus, results in more stable carbon and ash-forming minerals.|POSSIBLE APPLICATIONS OF AC|The availability of high surface area of particles possessed by AC as well its adsorptive ability makes it a significant constituent in many industries. Industries like; petroleum, fertilizer plants, nuclear, pharmaceuticals, cosmetics, textiles, automobile, and vacuum manufacturing all uses AC. AC has found to be good porous materials, which make it very effective in adsorption of solutes from aqueous solutions.|This was suggested to be due to the possession of large specific surface area. Furthermore, it has been extensively used for; Additionally, in a novel low-cost process developed for treating leach ate using AC placed in a contactor laboratory plastic column), optimum pollutant removal efficiencies for BOD5, COD, TDS, TSS and pH were observed and the results revealed that AC filtration had an effect on the removal of pollutants after electrolysis, though the overall performance of the treatment using AC depends on the concentration and chemical composition of the effluent contents As environmental pollution is becoming a more serious problem which needs attention of researchers, the need for AC is therefore growing all over the globe.|Moreover, in a study conducted by Khaleel et al. using coconut and palm shell granular activated carbon to treat institution water yielded that, both GACC and GACP can be used to remove high ratios of BOD, turbidity, TDS, TSS and COD from wastewater. In addition, the findings of Khaleel et al. suggested that a simple pre-treatment like electrolysis can be conducted on the wastewater to be treated prior to using the GACC or GACP so as to get higher removal efficiencies for the various pollutants present. The results of experiments utilizing GAC prepared from coconut shell (GACC) and GAC from palm shell (GACP) were presented to reduce BOD, COD, turbidity, TDS, TSS and pH in wastewater.|A comparison of these two techniques was undertaken to identify ways to improve the efficiency of the treatment process. The adsorptive, catalytic, electrochemical and other useful properties of AC are significantly influenced by its chemical nature. In general, AC having acidic chemical property is promising for basic gas adsorption, example ammonia.|For acidic gas adsorption like sulfur dioxide, the AC having basic chemical properties is appropriate. It was successful using AC in the adsorption of phenol and its derivatives.presents machineries required in setting an AC plant.|RESULTS AND DISCUSSION FTIR ANALYSIS|FTIR FOR AZADIRACHTA INDICA WOODS POWDER|FT-IR spectra of synthesized pure & copper doped ZnO NPs using zinc acetate before and after Thermal Analysis result of as synthesized oxides of a) ZnO and b) Zn calcination. The intense absorption peaks in the region 430-520 cm-1 correspond to the standard peak of ZnO due to ZnO stretching frequency of Zn– O bonds confirm the presence of M–O vibration bands, and the wide absorption near 3430 cm-1 was due to O-H stretching vibrations. The absorption occurred around 1614 cm-1 was due to aromatic C=Cring stretching while the strong intensity at 1401 cm-1was due to a-CH2 bending vibrations of aldehydes and ketones.|SEM ANALYSIS|SEM FOR AZADIRACHTA INDICA WOOD POWDER|SEM micrographs of the Azadirachta indica wood powder showed that the powder was an assemblage of fine particles, which did not have regular, fixed shape and size. Some of the particles may be quite small while some others may be as big 10µm in diameter. All the particles have broken edges with steps and kinks contributing to the uneven topography. The surface appeared as a fibrous material with irregular macro-pores and some expanded cavities which may allow for the diffusion of the molecules through the macro-pores of the adsorbent.|SEM FOR ACTIVATED CARBON|The spot size produced from the gun is too large to generate a sharp image therefore the SEM equipped with the lenses to compress the spot and direct the focused electron on the Specimen.|The spot size of most SEMs is less than (10 nm) with electrons collected from the final lens interact with the specimen and penetrate to a depth of (1µm) to generate the signals used to produce an image.|The image of the specimen is formed point by point depending on the movement of the scan coils, which cause the electron beam to move to discrete locations in a form of straight lines until a rectangular raster is produced on the surface of the specimen.|All the process depends on magnification required. In case when the operator requests a higher magnified image, the scan coils make the beam to deflect a cross a smaller area. It is worth mentioning that the working distance, which is the distance from the last lens to the surface of the specimen, has an effect on the magnification, in which in the modern SEM this is solved by automatic adjustment.|Scanning electron microscopy (SEM) is used to study the surface topography of any solid material. It shows better results than optical microscopy because of its high and better resolution and enhanced depth of field.|SEM photographs were taken with scanning electron micro scope at the required magnification at room temperature. The working distance of 7mm was maintained and acceleration voltage used was 5–20 kV at different magnification, with the secondary electron image (SEI) as a detector.|PREPARATION OF CUSO4 COPPER SULFATE|The heavy metal cuso4 Copper sulfate were collected at department of chemical engineering laboratory, Karur district and it was taken cuso4 10gm dilute in 500ml.|BY USING A ACTIVATED CARBON T0 REMOVAL OF CUSO4 COPPER SULFATE|It was taken 25ml of heavy metal and 0.5gm of activated carbon with 25ml of distillate water to prepare colloidal solution, and the removal of heavy metal in colloidal solution by using a filter paper.|CALCULATION FOR T0 REMOVAL OF CUSO4 COPPER SULFATE|1. The heavy metal CUSO4 Copper sulfate = 25Ml|2. The distillate water = 25Ml|3. The activated carbon = 0.5gm|TABULATION-1|Table :|THE HIGHEST REMOVAL PERCENTAGE OF CUSO4 COPPER SULFATE = 96 %|CONCLUSION|The Azadirachta indica wood commonly available waste material in tamil - nadu.|It is useful in medicine, but utilization of Azadirachta indica wood using various treatments can be used as a low cost adsorbent instead of high cost adsorbent.|The surface area and particle size are 421 m2 /g and 5um respectively also studied. In the present work the Azadirachta indica wood Powder converted into the activated carbon by chemical method. The results of this study have shown that activated carbon had a good effect on improving the adsorption capacity and chemical strength of based adsorbent.|This can improve the effective sites and functional groups on the adsorbent surface, thus improving its industrial effluent adsorption capacity.|The importance of operating conditions on industrial effluent adsorption by activated carbon can be arranged in the order of adsorption time less then dosage less then pH less then temperature. (IN202441053277)|The Azadirachta indica wood were collected at hometown, Erode district and it was crushed into small pieces, and then washed repeatedly with tap water for 5 times and distilled water for 3 times because of removing unwanted dust particles and impurities in the leaves. Then it was dried in sunlight as well as in hot air oven for 2 hours and then grinded in ball mill for getting a raw material as a powder form.|PREPARATION OF ACTIVATED CARBON|Initially Azadirachta indica woods were washed repeatedly by using distilled water to remove moisture and soluble impurities. Then Azadirachta indica woods kept in oven at 900C, for 2-3 hrs till leaves turn pale Green. Then crushed and screen by 10-15 and kept in oven 20-25 minute. After drying powder was mixed with KOH in silica crucible and kept in furnace at 2600C for 4 hrs The heating period depend on atmospheric temperature then solution was cooled & repeatedly washed using hot water to remove free acid and moisture, total 11 washing taken and kept it in oven for 20-25 minute the prepared brown colored adsorbent kept in bottle for further Characterization process use.|About 20 gm sample and 10ml KOH taken in silica crucible and kept in furnace. The furnace is initially at normal room temperature then furnace set at 2600C. Heating was carried out for 4 Hour. Then sample was removed and cool. After cooling the sample was repeatedly washed for 11 times using hot water to remove free acid and moisture. Then sample kept in oven for 20-25 minute and the activated black colored adsorbent stored in bottle for further Characterization process use.|MATERIALS|MATERIAL USED|- Water|- Clay|- Azadirachta indica wood|CHEMICAL USED|- Ethanol|- KOH|EQUIPMENT USED|- Ball mill|- Hot air oven|- Muffle furnace|- Magnetic stirrer|- Centrifuge|ANALYTIC EQUIPMENT USED|- FT-IR|- SEM|Types of Adsorption|There are two types of Adsorption a. Physical Adsorption or Physiosorption b. Chemical Adsorption or Chemisorption.|The presence of heavy metals water has become a major problem in today’s world due to its direct effect on all living organisms especially on human beings. If these present in quantities above a certain permissible limit, they can cause various short and long-term hazardous and harmful effects, such as shortness of breath and lungs, coughing, and wheezing leading to gastrointestinal effects, such as abdominal pain, vomiting, hemorrhage, and neurological effects.|Waste streams containing various heavy metals such as Pb, Cd, Cr, Cu, Zn, Ni are often encountered in various chemical and biochemical industries. Activated carbon has been also used as a natural.|Adsorbent for the removal of industrial effluent, but it is readily soluble under extreme pH conditions and also not cost effective. Other alternative materials such as Neem leaves, papaya seeds, rice husk and banana peel, carbon fly ash, cork waste, bagasse fly ash, groundnut shell, coconut have also been investigated.|These materials are waste products from industries and act as natural adsorbents. Under optimum conditions, they can exhibit up to 99%removal of heavy metal. These adsorbents are show high adsorption efficiency, easily available, economic and thus are more effective in the removal of heavy metals. Among all the natural adsorbents the Azadirachta Indica (neem) leaves has high potential to remove the heavy metals from effluent.|In India, Azadirachta indica (neem) is a tree which is commonly seen is all where India, the leaves of this tree is burnt and the burnt carbon can be utilized for the treatment and purification of water at a low cost without heavy operation. Heavy metal has been removed by neem leaves powder.|Some of the study reports the biosorption kinetics and the biosorption equilibrium of Zinc by Neem leaves and stem bark powder. Neem bark powder (NBP) has been used as an adsorbent for the removal of heavy metals from aqueous solutions.|The potentiality of Neem has also been widely studied by different researchers for solving most of the problems related to agriculture, environmental pollution public health, population control.|Hence in this present study, the Azadirachta indica (Neem) leaf powder is studied for his adsorptive capacity to remove metals from aqueous solution|ACTIVATED CARBON|The origin of activated carbon (AC) is associated with Ancient Egypt (1500 BC), whereby the Egyptians make use of its adsorbent characteristics for water purifications and medicinal purposes. During the last few years, adsorption of gases on charcoal has been reported by a Swedish chemist, Kar Wilhelm. Within recent decades, the AC was used in industries as a decolorizing agent. However, the potential use of AC was actually capitalized during the First World War, where by AC was used in gas mask against toxic gases. Respiratory protective devices were developed as personal protective tools against the use of toxic gases during wars. Hence, granular activated carbon (GAC) has found application during the first World War and still been used nowadays.|During the beginning of 20th century, the first AC production plant was commissioned in Germany purposely for a sugar refining industry. Lately, some of the plants emerged to produce AC for wastewater treatment processes. Recently, the AC is abundantly utilized as an air purifier in atmospheric air contaminant cleaning, color removal of industrial and automobile exhaust, food and pharmaceutical products also used as refrigerator deodorizers and in advanced applications such as nuclear plants. In the late 1930’s undoubtedly, AC gained huge momentum and popularity in industrial sectors, for both gaseous and aqueous phase applications. In fact, various new carbon production processes were developed to meet the continuous increasing industrial needs.|Within the period of 1939 to 1945, a considerable advancement took place whereby several chemically saturated carbon were produced for war and nerve gases trapping. As of 2014, the estimated amount of AC was assumed to be about 1.1 million metric tons from AC industries with a 10% increase in the projected demand for fresh AC. there will be an expected increase in demand for AC in the United States of America (USA) due to the new federal laws directing removal of heavy metals from coal-fed power plants|PYROLYSIS PROCESS|Thermo chemical conversion of organic biomass into gaseous or/and liquid fuels at extremely high temperature in the absence of halogen (mainly oxygen) is termed as pyrolysis. Pyrolysis is a simultaneous process that changes both the chemical composition and physical phase of materials and is irreversible. Pyrolysis process is mostly observed when materials are exposed to higher temperatures. Some features of pyrolysis such as temperature has the most significant effect and then followed by retention time, heating rate and nitrogen flow rate. Normally, when the reaction temperature increased, causes reduction in both AC and char production, while at the same time increasing the pyrolysis temperature leads to a drop off of solid yield and an increase in both gases and liquid percentages yield. On the other hand, raising the temperature leads to raised ash and AC percentage, whereas the volatile matter gets reduced. Therefore, AC with greater quality is obtained at a higher temperature. Moreover, increasing the temperature that eventually decreases char yield could also be because of major decomposition of biomass at elevated temperatures or in the course of secondary decomposition of char residues. At the same time, higher temperatures at which secondary decomposition occurs could lead to getting some gaseous products that are non-condensable and ultimately increasing gas yield. Presents laboratory setup for the activated reactor and fixed-bed pyrolysis.|PHYSICAL ACTIVATION PROCESS|Physical activation is a two-step process. Carbonization of carbonaceous materials comes first, then activation of the resulting char at high temperatures in the presence of CO2, steam, air or three mixtures serving as oxidizing gases.|The CO2 is usually used as activation gas being easy to handle, clean and possesses a slow reaction rate at a temperature process. A temperature range of 400°C and 850°C was found to be the carbonization temperature, though it may sometimes reach up to 1000°C while activation temperature between 600°C and 900°C.|CHEMICAL ACTIVATION PROCESS|In the chemical activation process, involves multiple two steps occurring simultaneously, with the chemical activating agents mixing with the precursor, as oxidants and dehydrates. Performing activation and carbonization simultaneously during the chemical activation process at lower temperature results in having better porous structures of AC, even though, concern about environmental protection may limit the use of chemical agents for activation. Moreover, some chemicals that are widely used as activating agents are zinc chloride (ZnCl2), potassium hydroxide (KOH), trihydroxidooxido phosphorus, phosphoric acid (H3PO4) and potassium carbonate (K2CO3). Whereas the agricultural wastes that are being reduced with the earlier mentioned chemicals consist of; olive seed, apricot stones, macadamia, pecan-shells, peanut-hulls, nut- shells, almond shells, corn-cob, hazelnut shells, rice husks, rice straw and Cassava peel.|STEAM PYROLYSIS|In this process, the raw agricultural waste materials are either heated at a temperature range of 500–700°C under a flow of pure steam or heated at a higher temperature range of 700– 800°C under a flowing steam. Steam pyrolysis has been widely studied and successfully applied on various types of agricultural waste biomass such as rice husk, jujube seed, sawdust, tropical wood waste, palm shells, durian peel, corn cobs, coconut shells, tobacco stems, hazelnut shell, banana peels, mangosteen shells, etc.|However, the AC produced by steam pyrolysis was generally reported to be less effective, with an exception of those produced from cherry stones, apricot and almond shell. the ultimate and proximate analysis of agricultural residues as they are generated in large quantity worldwide.|FACTORS AFFECTING AC PRODUCTION:|RAW MATERIALS|Most organic substances with high carbon content are potential raw materials for AC production. To produce a porous carbon structure, the under listed factors can be considered.|- High carbon content|- Low inorganic content (i.e. low ash)|- Potential extent of activation|- Low degradation upon storage|- High density and sufficient volatile content|- Stability of supply in the countries|- Inexpensive materials.|Lignocelluloses materials were generally accepted as precursor for AC production and constitute about 45% of the total raw materials used. The characteristics of some raw materials used in the AC production. To produce AC with low ash content, it is important to get materials with low inorganic content. Full control of the manufacturing process requires a moderately high volatile content. Coconut shell and fruit stones are the most commonly raw materials. This might be because of their hardness, volatile content, and relatively high density, and content, which make them most prepared for hard GAC production. Moreover, other materials for example coconutshell, olive stones and peach waste are commercially utilized for micro-porous AC production and as well find usage for a variety of applications.|TEMPERATURE|In the AC production, the activation temperature plays a vital role in affecting the characteristic of the AC produced. As for commercial purposes AC, it is normally carried out in a mixture of steam and CO2 at a temperature above 800°C. In recent times, researchers have been up-and-doing to optimize final activation temperature in order to reduce cost and period of AC production. Several studies have been reported which indicated that activation temperature has great influence surface area and production yield of AC. The activation temperature is between 200 to 1100°C. However, a temperature range of 400 to 500°C was reported by previous researchers to be considered regardless of time taken and the impregnation ratio for a variety of raw materials. Therefore, increasing activation temperature always results in the reduction of AC yield during production, which at the same time results in increasing the volume of volatile substances released. Generally, it is inappropriate to prepare AC at a temperature above 800°C.|This goes along with an increase of fixed carbon and ash content, which may be ascribed to the removal of volatile matter in the material during carbonization process. Thus, results in more stable carbon and ash-forming minerals.|POSSIBLE APPLICATIONS OF AC|The availability of high surface area of particles possessed by AC as well its adsorptive ability makes it a significant constituent in many industries. Industries like; petroleum, fertilizer plants, nuclear, pharmaceuticals, cosmetics, textiles, automobile, and vacuum manufacturing all uses AC. AC has found to be good porous materials, which make it very effective in adsorption of solutes from aqueous solutions.|This was suggested to be due to the possession of large specific surface area. Furthermore, it has been extensively used for; Additionally, in a novel low-cost process developed for treating leach ate using AC placed in a contactor laboratory plastic column), optimum pollutant removal efficiencies for BOD5, COD, TDS, TSS and pH were observed and the results revealed that AC filtration had an effect on the removal of pollutants after electrolysis, though the overall performance of the treatment using AC depends on the concentration and chemical composition of the effluent contents As environmental pollution is becoming a more serious problem which needs attention of researchers, the need for AC is therefore growing all over the globe.|Moreover, in a study conducted by Khaleel et al. using coconut and palm shell granular activated carbon to treat institution water yielded that, both GACC and GACP can be used to remove high ratios of BOD, turbidity, TDS, TSS and COD from wastewater. In addition, the findings of Khaleel et al. suggested that a simple pre-treatment like electrolysis can be conducted on the wastewater to be treated prior to using the GACC or GACP so as to get higher removal efficiencies for the various pollutants present. The results of experiments utilizing GAC prepared from coconut shell (GACC) and GAC from palm shell (GACP) were presented to reduce BOD, COD, turbidity, TDS, TSS and pH in wastewater.|A comparison of these two techniques was undertaken to identify ways to improve the efficiency of the treatment process. The adsorptive, catalytic, electrochemical and other useful properties of AC are significantly influenced by its chemical nature. In general, AC having acidic chemical property is promising for basic gas adsorption, example ammonia.|For acidic gas adsorption like sulfur dioxide, the AC having basic chemical properties is appropriate. It was successful using AC in the adsorption of phenol and its derivatives.presents machineries required in setting an AC plant.|RESULTS AND DISCUSSION FTIR ANALYSIS|FTIR FOR AZADIRACHTA INDICA WOODS POWDER|FT-IR spectra of synthesized pure & copper doped ZnO NPs using zinc acetate before and after Thermal Analysis result of as synthesized oxides of a) ZnO and b) Zn calcination. The intense absorption peaks in the region 430-520 cm-1 correspond to the standard peak of ZnO due to ZnO stretching frequency of Zn– O bonds confirm the presence of M–O vibration bands, and the wide absorption near 3430 cm-1 was due to O-H stretching vibrations. The absorption occurred around 1614 cm-1 was due to aromatic C=Cring stretching while the strong intensity at 1401 cm-1was due to a-CH2 bending vibrations of aldehydes and ketones.|SEM ANALYSIS|SEM FOR AZADIRACHTA INDICA WOOD POWDER|SEM micrographs of the Azadirachta indica wood powder showed that the powder was an assemblage of fine particles, which did not have regular, fixed shape and size. Some of the particles may be quite small while some others may be as big 10µm in diameter. All the particles have broken edges with steps and kinks contributing to the uneven topography. The surface appeared as a fibrous material with irregular macro-pores and some expanded cavities which may allow for the diffusion of the molecules through the macro-pores of the adsorbent.|SEM FOR ACTIVATED CARBON|The spot size produced from the gun is too large to generate a sharp image therefore the SEM equipped with the lenses to compress the spot and direct the focused electron on the Specimen.|The spot size of most SEMs is less than (10 nm) with electrons collected from the final lens interact with the specimen and penetrate to a depth of (1µm) to generate the signals used to produce an image.|The image of the specimen is formed point by point depending on the movement of the scan coils, which cause the electron beam to move to discrete locations in a form of straight lines until a rectangular raster is produced on the surface of the specimen.|All the process depends on magnification required. In case when the operator requests a higher magnified image, the scan coils make the beam to deflect a cross a smaller area. It is worth mentioning that the working distance, which is the distance from the last lens to the surface of the specimen, has an effect on the magnification, in which in the modern SEM this is solved by automatic adjustment.|Scanning electron microscopy (SEM) is used to study the surface topography of any solid material. It shows better results than optical microscopy because of its high and better resolution and enhanced depth of field.|SEM photographs were taken with scanning electron micro scope at the required magnification at room temperature. The working distance of 7mm was maintained and acceleration voltage used was 5–20 kV at different magnification, with the secondary electron image (SEI) as a detector.|PREPARATION OF CUSO4 COPPER SULFATE|The heavy metal cuso4 Copper sulfate were collected at department of chemical engineering laboratory, Karur district and it was taken cuso4 10gm dilute in 500ml.|BY USING A ACTIVATED CARBON T0 REMOVAL OF CUSO4 COPPER SULFATE|It was taken 25ml of heavy metal and 0.5gm of activated carbon with 25ml of distillate water to prepare colloidal solution, and the removal of heavy metal in colloidal solution by using a filter paper.|CALCULATION FOR T0 REMOVAL OF CUSO4 COPPER SULFATE|1. The heavy metal CUSO4 Copper sulfate = 25Ml|2. The distillate water = 25Ml|3. The activated carbon = 0.5gm|TABULATION-1|Table :|THE HIGHEST REMOVAL PERCENTAGE OF CUSO4 COPPER SULFATE = 96 %|CONCLUSION|The Azadirachta indica wood commonly available waste material in tamil - nadu.|It is useful in medicine, but utilization of Azadirachta indica wood using various treatments can be used as a low cost adsorbent instead of high cost adsorbent.|The surface area and particle size are 421 m2 /g and 5um respectively also studied. In the present work the Azadirachta indica wood Powder converted into the activated carbon by chemical method. The results of this study have shown that activated carbon had a good effect on improving the adsorption capacity and chemical strength of based adsorbent.|This can improve the effective sites and functional groups on the adsorbent surface, thus improving its industrial effluent adsorption capacity.|The importance of operating conditions on industrial effluent adsorption by activated carbon can be arranged in the order of adsorption time less then dosage less then pH less then temperature. Family Number|(110856270)|110856270|Abstract|(IN202441053277 A)|This study explores the preparation and characterization of activated carbon derived from “Azadirachta indica” wood, a widely available waste material in Tamil Nadu, India. With increasing industrialization, the management of heavy metal contamination has become critical. This research aims to utilize “Azadirachta indica” wood as a sustainable and cost-effective adsorbent for the removal of copper sulfate (CuSO4) from aqueous solutions. The methodology involved the collection of “Azadirachta indica” wood, which was subsequently crushed and thoroughly washed to eliminate dust and impurities. The wood was dried using sunlight and a hot air oven, then ground into a fine powder. For the activation process, the wood was treated with potassium hydroxide (KOH) and subjected to high temperatures (2600°C) in a furnace for a specified duration. Following activation, the product was washed multiple times with hot water to remove free acids and moisture, resulting in a brown-colored activated carbon ready for characterization. Characterization techniques employed included Fourier Transform Infrared Spectroscopy (FTIR) and Scanning Electron Microscopy (SEM). FTIR analysis revealed significant absorption peaks corresponding to functional groups associated with activated carbon, such as O-H stretching and C=O vibrations. SEM images displayed a porous structure with irregular particles, highlighting the effective surface area available for adsorption. The effectiveness of the activated carbon as an adsorbent was evaluated through a series of batch adsorption experiments with varying concentrations of CuSO4. The results indicated a maximum removal efficiency of 96% when 0.5 grams of activated carbon were used in a 25 mL solution of CuSO4. This demonstrates the high adsorption capacity of the activated carbon produced from “Azadirachtaindica”wood, underscoring its potential for treating industrial effluents. Furthermore, the study examined the influence of various operational parameters such as dosage, pH, and contact time on the adsorption efficiency. The optimal conditions were determined, with the results suggesting that the order of significance for the adsorption process is as follows: adsorption time > dosage > pH > temperature. This information can guide practical applications in effluent treatment systems. In conclusion, this research highlights the viability of utilizing “Azadirachta indica” wood as an effective and low-cost adsorbent for heavy metal removal. The findings contribute to environmental sustainability by promoting the use of agricultural waste in waste management processes. Future studies may focus on scaling up this process and exploring other waste materials for activated carbon production, further enhancing the feasibility of sustainable adsorbents in industrial applications. Keywords: Adsorption, azadirachta indica wood powder, cuso4, Freundlich and Langmuir Isothermetting a raw material as a powder form.|IPC codes|(IN202441053277 A)|B01J-020/02|B01J-020/34|Title|(IN202441053277 A)|Synthesis of activated carbon for the removal of heavy metals from the aqueous solution| Chemical engineering|Environmental technology B01J-020/02|B01J-020/34|C02F-001/28|C02F-101/20 B01J-020/02|B01J-020/34|C02F-001/28|C02F-101/20 PENDING (IN202441053277)|PENDING ALIVE (IN202441053277)|ALIVE (IN202441053277)|LEGAL DETAILS FOR IN202441053277|Actual or expected expiration date=2044-07-12|Legal state=ALIVE|Status=PENDING|Event publication date=2024-07-12|Event code=IN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=IN IN202441053277|Application date=2024-07-12|Standardized application number=2024IN-41053277|Event publication date=2024-07-26|Event code=IN/A|Event indicator=Pos|Event group=Examination events|Application laid open|Publication country=IN|Publication number=IN202441053277|Publication stage code=A|Publication date=2024-07-26|Standardized publication number=IN202441053277 (IN202441053277)|IN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=/WizbbSQlgu604esobGCR85XA5Cblt0Ya/WZFbsCsqzB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=IN0000000001511247&ekey=2383&xpn=IN202441053277&kind=A https://iprsearch.ipindia.gov.in/PublicSearch/PublicationSearch/ApplicationStatus https://permalink.orbit.com/RenderStaticFirstPage?XPN=dR15du4ks0tz814XOkcH0cExnvIz5kLrfqHome9U%252B8A%3D%26n%3D1&id=0&base=FAMPAT IN (IN202441053277)|NAME=Gunasekaran Gnanapragasam|NAME=Anbu A|NAME=Gowrishankar R|NAME=Premkumar G|NAME=Thaarun S|NAME=Mappilaimeeran S|NAME=Saravanan S 0 1 Titre: (IN202441053277)|Synthesis of activated carbon for the removal of heavy metals from the aqueous solution Résumé: (IN202441053277)|This study explores the preparation and characterization of activated carbon derived from “Azadirachta indica” wood, a widely available waste material in Tamil Nadu, India. With increasing industrialization, the management of heavy metal contamination has become critical. This research aims to utilize “Azadirachta indica” wood as a sustainable and cost-effective adsorbent for the removal of copper sulfate (CuSO4) from aqueous solutions. The methodology involved the collection of “Azadirachta indica” wood, which was subsequently crushed and thoroughly washed to eliminate dust and impurities. The wood was dried using sunlight and a hot air oven, then ground into a fine powder. For the activation process, the wood was treated with potassium hydroxide (KOH) and subjected to high temperatures (2600°C) in a furnace for a specified duration. Following activation, the product was washed multiple times with hot water to remove free acids and moisture, resulting in a brown-colored activated carbon ready for characterization. Characterization techniques employed included Fourier Transform Infrared Spectroscopy (FTIR) and Scanning Electron Microscopy (SEM). FTIR analysis revealed significant absorption peaks corresponding to functional groups associated with activated carbon, such as O-H stretching and C=O vibrations. SEM images displayed a porous structure with irregular particles, highlighting the effective surface area available for adsorption. The effectiveness of the activated carbon as an adsorbent was evaluated through a series of batch adsorption experiments with varying concentrations of CuSO4. The results indicated a maximum removal efficiency of 96% when 0.5 grams of activated carbon were used in a 25 mL solution of CuSO4. This demonstrates the high adsorption capacity of the activated carbon produced from “Azadirachtaindica”wood, underscoring its potential for treating industrial effluents. Furthermore, the study examined the influence of various operational parameters such as dosage, pH, and contact time on the adsorption efficiency. The optimal conditions were determined, with the results suggesting that the order of significance for the adsorption process is as follows: adsorption time > dosage > pH > temperature. This information can guide practical applications in effluent treatment systems. In conclusion, this research highlights the viability of utilizing “Azadirachta indica” wood as an effective and low-cost adsorbent for heavy metal removal. The findings contribute to environmental sustainability by promoting the use of agricultural waste in waste management processes. Future studies may focus on scaling up this process and exploring other waste materials for activated carbon production, further enhancing the feasibility of sustainable adsorbents in industrial applications. Keywords: Adsorption, azadirachta indica wood powder, cuso4, Freundlich and Langmuir Isothermetting a raw material as a powder form. 121 Abstract gpt-4o-mini no The article focuses on the synthesis of activated carbon for heavy metal removal, which does not relate to accelerated weathering or CO₂ capture.
124 CN201510132681 CN201510132681 CN104803381|CN104803381 70372919 CN104803381 B 2016-08-17 [CN104803381B]|CN104803381 A 2015-07-29 [CN104803381] 2015-03-25 2015-03-25 2016-08-17|2015-07-29 (CN104803381B)|2016-08-17 (CN104803381)|2035-03-25 (CN104803381)|Method for preparing activated carbon from Hunan oil tea shells, activated carbon and application of activated carbon (CN104803381)|The invention relates to a method for preparing activated carbon from Hunan camellia oleifera shells, activated carbon and an application of the activated carbon, and belongs to the field of biochemical engineering. The method comprises the following steps: the Hunan camellia oleifera shells are dried, crushed and sieved; Hunan camellia oleifera shell powder is dipped with aqueous alkali; the dipped Hunan camellia oleifera shell powder is subjected to primary activation with microwaves, the temperature for the primary activation is 200-450 DEG C, and the primary activation is performed for 0.5-2 h; the Hunan camellia oleifera shell powder after the primary activation is carbonized and ground to obtain powdered carbon; a strong acid solution is added to the powdered carbon, ash removal is performed through microwave heating at the temperature of 200-450 DEG C for 0.5-1 h, and the powdered carbon after ash removal is washed to neutral; 1-5 times of mass of water is added to the powdered carbon after washing, the mixture is subjected to secondary activation with microwaves until the mixture is dried, then the activated carbon is obtained, and the temperature for the secondary activation is 200-450 DEG C. The activated carbon prepared with the method is applicable to a supercapacitor. CHANGSHA GUO RONG NEW FORMS OF ENERGY (CN104803381)|Changsha Guo Rong new forms of energy Co., Ltd ([CN])|(CN104803381)|Changsha Guo Rong new forms of energy Co., Ltd XIE RONGAN|LIU DENGYOU|LI ZHIGUANG|ZHOU ZHI|DONG XINRONG|LIN ZHONGFU|WANG GUOQING|SONG YUNFENG|KUANG HAO|WU LIJUN (CN104803381)|XieRong An|Liu Dengyou|Li Zhiguang|Zhou Zhi|DONG XINRONG|Lin Zhongfu|Wang Guoqing|SONG YUNFENG|Kuang Hao|WU LIJUN|(CN104803381)|XIE RONGAN|LIU DENGYOU|LI ZHIGUANG|ZHOU ZHI|DONG XINRONG|LIN ZHONGFU|WANG GUOQING|SONG YUNFENG|KUANG HAO|WU LIJUN (CN104803381)|LU HONG;CHANGSHA ZONEKEY PATENT LAW FIRM|Reg. Nb: 43113 (CN104803381)|The method for preparing the activated carbon by using the biomass as the raw material has the advantages of rich and reproducible resources, meets the requirement of low-carbon social development, and gradually becomes a hotspot of research and development of people.|The super capacitor is used as a storage and conversion mode of energy, and has the advantages of high charging speed, high power, long service life and the like, so that the super capacitor is widely applied to electronic products (a coordinator and a computer storage), and is also beginning to be applied to energy supplement and recovery of electric automobiles, cranes, subways and the like.|Energy and environmental problems are important problems facing the world and are in a trend of increasing severity, and thus, countries are forced to search new energy and new energy conversion and storage modes.|The resin activated carbon has stable performance, but the resin preparation technology is complex and the price is expensive.| (CN104803381)|1. A method for preparing activated carbon by using Hunan oil tea shells is characterized by comprising the following steps:(1) drying, crushing and sieving Hunan oil-tea camellia shells to obtain Hunan oil-tea camellia shell powder;(2) dipping the Hunan oil-tea camellia fruit shell powder by using an alkali solution, wherein the alkali solution is a 2-5 wt% NaOH or KOH solution;(3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 200-450 ℃, and the time is 0.5-2 h;(4) carbonizing the once activated Xiang oil tea fruit shell powder, and crushing to obtain carbon powder;(5) adding a strong acid solution into the carbon powder, performing microwave heating for ash removal at the temperature of 200-450 ℃ for 0.5-1 h, and washing the carbon powder to be neutral by using water after ash removal;(6) adding water with the mass being 1-5 times that of the carbon powder into the washed carbon powder, and performing secondary activation by using microwaves until the carbon powder is dried to obtain activated carbon, wherein the temperature of the secondary activation is 200-450 ℃.| (CN104803381)|The invention further provides a method for producing the activated carbon by using the Hunan oil-tea camellia shells.|The invention relates to a method for preparing activated carbon by using Hunan oil tea shells, the activated carbon and application thereof, and belongs to the field of biochemical engineering.| (CN104803381)|ACTIVATED CARBON(100,50)|TEA SHELL(100,10)|XIANG OIL TEA FRUIT(100,6)|OIL TEA CAMELLIA FRUIT(74,14)|CAMELLIA FRUIT(73,14)|TEA FRUIT(65,8)|SEVERITY TREND(59,1)|REPRODUCIBLE RESOURCE(56,1)|CARBON POWDER(53,17)|RESEARCH HOTSPOT(53,1)|SUPERCAPACITOR(47,9)|XIANG OIL(44,9)|ASH REMOVAL(43,12)|BIOCHEMICAL ENGINEERING(42,2)|PRIMARY ACTIVATION(41,13)|CAMELLIA SHELL(41,2)|OIL TEA CAMELLIA SHELL(41,2)|ALKALI SOLUTION(40,5)|WASHED CARBON POWDER(40,3)|TEA FRUIT SHELL(37,4)|PEOPLE DEVELOPMENT(37,1)|SUPPLEMENTING ENERGY(34,1)|COORDINATOR(30,1)|ELECTRIC AUTOMOBILE RECOVERY(28,1)|BIOMASS(27,1)|CRUSHING(25,6)|KOH SOLUTION(25,2)|SUBWAY(25,1)|PRICE(24,1)|CONVERSION MODE(22,1)|CRANE(22,1)|SOCIAL DEVELOPMENT(20,1)|LONG SERVICE LIFE(19,1)|RESIN ACTIVATED CARBON(19,1)|CAMELLIA OLEIFERA SEED BYPRODUCT(18,1)|IMMERSION TEMPERATURE(18,1)|CARBONIZATION TEMPERATURE(17,2)|RICH(17,1)|STORAGE MODE(17,1)|XIANG CAMELLIA OLEIFERA SHELL(17,1)|MICROWAVE HEATING(16,13)|STRONG ACID SOLUTION(16,5)|ELECTRIC AUTOMOBILE(16,1)|H2SO4AND(15,2)|CARBONIZATION FURNACE(13,3)|ENERGY CONVERSION(13,1)|CHARGING SPEED(12,1)|104HM2ANNUAL OIL TEA FRUIT(11,1)|COMPUTER STORAGE(10,1)|ELECTRONIC PRODUCT(10,1)|DRYING XIANG OIL(9,3)|SODIUM HYDROXIDE(9,2)|AGRICULTURE BYPRODUCT(9,1)|RICH RESOURCE(8,2)|LOW CARBON SOCIAL DEVELOPMENT(8,1)|NONCARBON IMPURITY(8,1)|NONRENEWABLE RESOURCE(8,1)|SUPERCAPACITOR REQUIREMENT(8,1)|MESH SIEVE(7,3)|CARBONIZATION TIME(7,2)|HYDROGEN CHLORIDE(6,6)|WOODY OIL CROP(6,2)|LIGNIN DEGRADATION(6,1)|XIANG TEA OIL TREE(6,1)|MEDIAN PORE DIAMETER(5,3)|SUPERCAPACITOR ACTIVATED CARBON(5,3)|ALMOND SHELL(5,1)|MICROWAVE ACTIVATION(5,1)|MICROWAVE ASSISTED ACTIVATION(5,1)|NATURE SCIENCE EDITION(5,1)|OIL TEA INDUSTRY DEVELOPMENT(5,1)|POLAR SUBSTANCE(5,1)|RESOURCE DISTRIBUTION REGION(5,1)|RESOURCE UTILIZATION(5,1)|PARTICLE SIZE(4,8)|ENVIRONMENTAL POLLUTION(4,2)|GRAIN SIZE(4,2)|MESOPORE PROPORTION(4,2)|ADSORBENT(4,1)|ALKALI CONSUMPTION(4,1)|ALKALI SUBSTANCE(4,1)|CAPACITOR DETECTION2THE SPECIFIC CAPACITANCE(4,1)|CLIMATE REASON(4,1)|EARLY ELECTRODE(4,1)|LOW CARBON(4,1)|MICROPORE HOLE DIAMETER(4,1)|MULTILEVEL HOLE(4,1)|OIL TEA YIELD(4,1)|PROVINCE(4,1)||(CN104803381)|ACTIVATED CARBON(100,50)|TEA SHELL(100,10)|XIANG OIL TEA FRUIT(100,7)|TEA FRUIT(62,9)|SEVERITY TREND(46,1)|OIL TEA CAMELLIA FRUIT(44,14)|XIANG OIL(44,10)|CAMELLIA FRUIT(43,14)|REPRODUCIBLE RESOURCE(43,1)|CARBON POWDER(41,17)|RESEARCH HOTSPOT(41,1)|SUPERCAPACITOR(36,9)|ASH REMOVAL(33,12)|PRIMARY ACTIVATION(32,13)|BIOCHEMICAL ENGINEERING(32,2)|CAMELLIA SHELL(32,2)|OIL TEA CAMELLIA SHELL(32,2)|WASHED CARBON POWDER(31,3)|TEA FRUIT SHELL(29,4)|PEOPLE DEVELOPMENT(29,1)|ALKALI SOLUTION(26,5)|SUPPLEMENTING ENERGY(26,1)|COORDINATOR(23,1)|ELECTRIC AUTOMOBILE RECOVERY(22,1)|BIOMASS(21,1)|CRUSHING(19,6)|SUBWAY(19,1)|PRICE(18,1)|CONVERSION MODE(17,1)|CRANE(17,1)|LONG SERVICE LIFE(15,1)|RESIN ACTIVATED CARBON(15,1)|SOCIAL DEVELOPMENT(15,1)|CAMELLIA OLEIFERA SEED BYPRODUCT(14,1)|IMMERSION TEMPERATURE(14,1)|STRONG ACID SOLUTION(13,5)|CARBONIZATION TEMPERATURE(13,2)|RICH(13,1)|STORAGE MODE(13,1)|XIANG CAMELLIA OLEIFERA SHELL(13,1)|MICROWAVE HEATING(12,13)|ELECTRIC AUTOMOBILE(12,1)|H2SO4AND(11,2)|KOH SOLUTION(11,2)|CARBONIZATION FURNACE(10,3)|ENERGY CONVERSION(10,1)|CHARGING SPEED(9,1)|DRYING XIANG OIL(7,3)|AGRICULTURE BYPRODUCT(7,1)|COMPUTER STORAGE(7,1)|ELECTRONIC PRODUCT(7,1)|MESH SIEVE(6,3)|SODIUM HYDROXIDE(6,3)|RICH RESOURCE(6,2)|LOW CARBON SOCIAL DEVELOPMENT(6,1)|NONCARBON IMPURITY(6,1)|NONRENEWABLE RESOURCE(6,1)|SUPERCAPACITOR REQUIREMENT(6,1)|HYDROGEN CHLORIDE(5,6)|CARBONIZATION TIME(5,2)|WOODY OIL CROP(5,2)|LIGNIN DEGRADATION(5,1)|XIANG TEA OIL TREE(5,1)|MEDIAN PORE DIAMETER(4,3)|SUPERCAPACITOR ACTIVATED CARBON(4,3)|ALMOND SHELL(4,1)|MICROWAVE ACTIVATION(4,1)|MICROWAVE ASSISTED ACTIVATION(4,1)|NATURE SCIENCE EDITION(4,1)|OIL TEA INDUSTRY DEVELOPMENT(4,1)|POLAR SUBSTANCE(4,1)|RESOURCE DISTRIBUTION REGION(4,1)|RESOURCE UTILIZATION(4,1)|PARTICLE SIZE(3,8)|ENVIRONMENTAL POLLUTION(3,2)|GRAIN SIZE(3,2)|MESOPORE PROPORTION(3,2)|ADSORBENT(3,1)|ALKALI CONSUMPTION(3,1)|ALKALI SUBSTANCE(3,1)|CAPACITOR DETECTION2THE SPECIFIC CAPACITANCE(3,1)|CLIMATE REASON(3,1)|EARLY ELECTRODE(3,1)|HM2ANNUAL PRODUCTION(3,1)|LOW CARBON(3,1)|MICROPORE HOLE DIAMETER(3,1)|MULTILEVEL HOLE(3,1)|OIL TEA YIELD(3,1)|PROVINCE(3,1)| (CN104803381)|1. A method for preparing activated carbon by using Hunan oil tea shells is characterized by comprising the following steps:|(1) drying, crushing and sieving Hunan oil-tea camellia shells to obtain Hunan oil-tea camellia shell powder;|(2) dipping the Hunan oil-tea camellia fruit shell powder by using an alkali solution, wherein the alkali solution is a 2-5 wt% NaOH or KOH solution;|(3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 200-450 ℃, and the time is 0.5-2 h;|(4) carbonizing the once activated Xiang oil tea fruit shell powder, and crushing to obtain carbon powder;|(5) adding a strong acid solution into the carbon powder, performing microwave heating for ash removal at the temperature of 200-450 ℃ for 0.5-1 h, and washing the carbon powder to be neutral by using water after ash removal;|(6) adding water with the mass being 1-5 times that of the carbon powder into the washed carbon powder, and performing secondary activation by using microwaves until the carbon powder is dried to obtain activated carbon, wherein the temperature of the secondary activation is 200-450 ℃.|2. The method of claim 1, wherein the immersion temperature is 70 to 90 ℃ and the time is 7 to 24 hours.|3. The method according to claim 1, wherein in the step (1), the grain size of the Hunan oil tea fruit shell powder is 20-100 meshes.|4. The method according to claim 1, wherein the particle size of the carbon powder is 4-8 μm.|5. The method of claim 1, wherein the strong acid solution is 0.5 to 5wt% HCl or H2SO4And (3) solution.|6. The method according to claim 1, wherein the carbonization temperature is 700 to 900 ℃ and the carbonization time is 0.5 to 2 hours.|7. An activated carbon prepared from camellia oleifera Hunan shells, which is produced by the method of any one of claims 1 to 6.|8. The activated carbon of claim 7, wherein the pore size of the activated carbon is 3 to 4 nm.|9. Use of the activated carbon of claim 7 or 8 in a supercapacitor. (CN104803381)|TECHNICAL FIELD|[0002] The invention relates to a method for preparing activated carbon by using Hunan oil tea shells, the activated carbon and application thereof, and belongs to the field of biochemical engineering.|BACKGROUND ART|[0004] Energy and environmental problems are important problems facing the world and are in a trend of increasing severity, and thus, countries are forced to search new energy and new energy conversion and storage modes. The super capacitor is used as a storage and conversion mode of energy, and has the advantages of high charging speed, high power, long service life and the like, so that the super capacitor is widely applied to electronic products (a coordinator and a computer storage), and is also beginning to be applied to energy supplement and recovery of electric automobiles, cranes, subways and the like. Activated carbon was the earliest electrode material used in supercapacitors and is the only carbon material for double layer capacitors currently commercialized. The performance and price of activated carbon become key factors that restrict the development and application of supercapacitors.|[0005] The active carbon is mainly derived from three kinds, including biomass active carbon (fruit shell, tree, etc.), coal active carbon, and resin active carbon. The quality of coal-based activated carbon is influenced by the quality of coal, and particularly, the development of the coal-based activated carbon is restricted by the characteristics of limited resources and non-renewable resources. The resin activated carbon has stable performance, but the resin preparation technology is complex and the price is expensive. The method for preparing the activated carbon by using the biomass as the raw material has the advantages of rich and reproducible resources, meets the requirement of low-carbon social development, and gradually becomes a hotspot of research and development of people. Particularly, the fruit shell is used as a byproduct of agriculture, has extremely rich resources and a natural pore structure, and is a high-quality raw material for preparing the active carbon. However, the existing patent technology for preparing the super-capacitor activated carbon has the problems of large acid or alkali consumption and the like, for example, the acid concentration is up to 72% when the super-capacitor activated carbon is prepared by Chinese patent (CN 102205963A), and the mass ratio of the alkali carbon is up to 5:1 when the super-capacitor activated carbon is prepared by Chinese patent (CN 103539114A), so that the acid and alkali substances with high proportion are not only strong in corrosivity and easy to cause environmental pollution, but also directly cause higher production cost. Currently, coconut shells, almond shells and the like are used as main sources of supercapacitor active carbon, but the materials are influenced by climate reasons in China, and have strong regional resource distribution and limited sources.|[0006] The camellia oleifera shells are byproducts of camellia oleifera seeds after kernels are separated, the camellia oleifera is a special woody oil crop in China and mainly distributed in Hunan, Hubei, Guangdong, Guangxi, Fujian, Jiangxi and other provinces, the Hunan camellia oleifera shells are the camellia oleifera shells in the Hunan, and the area of the existing camellia oleifera in China is about 400 x 104hm2Annual oil tea fruit nearly 560 x 104t. In recent years, the development of the oil tea industry is vigorously promoted by China, and the yield of oil tea steadily increases year by year. The Hunan oil-tea camellia shells account for 60 percent of the weight of the oil-tea camellia fruits, and the resources are extremely rich. At present, most of Hunan oil tea shells are scattered in the hands of farmers, are basically used as fuels for baking in winter, have low added value and pollute the environment.|[0007] The Hunan oil tea fruit shell mainly comprises lignin, cellulose and the like, and is a high-quality raw material for preparing the activated carbon. With the enhancement of consciousness on resource utilization, people begin to use Hunan oil-tea camellia shells to prepare activated carbon for adsorption (a, Lijiaxing and the like, agricultural product processing (academic journal), 2013,10:20-24, b, horsepower and the like, grain and food industry, 2009,16(3):19-21, c, Longliujin and the like, Guangxi university report: Nature science edition, 2012,37(3):425 + 429), but the prepared activated carbon has poor quality and can only be used as an industrial adsorbent. Chinese patents (CN 102502628A, CN 103011155A) all adopt high-concentration phosphoric acid (80%) to treat Xiang tea-oil tree shells to prepare activated carbon for adsorption; chinese patent (CN 103030710A) adopts high-concentration zinc chloride (50%) or high-alkali carbon ratio (4:1) to process Xiang oil tea fruit shell to prepare activated carbon for adsorption. The technologies use high-concentration acid or high alkali-carbon ratio, belong to the traditional activated carbon preparation process, and have the problems of high cost, serious environmental pollution, low product quality and the like.|DISCLOSURE|[0008] Disclosure of Invention|[0009] The invention solves the technical problems of reducing the production cost of preparing the activated carbon by using Hunan oil-tea camellia shells and improving the product quality of the activated carbon.|[0010] The technical scheme of the invention is to provide a method for preparing activated carbon by using Hunan oil tea shells, which comprises the following steps:|[0011] (1) drying, crushing and sieving Hunan oil-tea camellia shells to obtain Hunan oil-tea camellia shell powder;|[0012] (2) dipping the Xiang oil tea fruit shell powder by using an alkali solution;|[0013] (3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 200-450 ℃, and the time is 0.5-2 h;|[0014] (4) carbonizing the once activated Xiang oil tea fruit shell powder, and crushing to obtain carbon powder;|[0015] (5) adding a strong acid solution into the carbon powder, performing microwave heating for ash removal at the temperature of 200-450 ℃ for 0.5-1 h, and washing the carbon powder to be neutral by using water after ash removal;|[0016] (6) adding water with the mass being 1-5 times that of the carbon powder into the washed carbon powder, and performing secondary activation by using microwaves until the carbon powder is dried to obtain activated carbon, wherein the temperature of the secondary activation is 200-450 ℃.|[0017] Further, the alkali solution is 2-5 wt% of NaOH or KOH solution.|[0018] Further, the dipping temperature is 70-90 ℃ and the time is 7-24 h.|[0019] Further, in the step (1), the grain size of the Hunan oil-tea camellia fruit shell powder is 20-100 meshes.|[0020] Further, the particle size of the carbon powder is 4-8 mu m.|[0021] Further, the strong acid solution is 0.5-5 wt% of HCl or H2SO4And (3) solution.|[0022] Further, the carbonization temperature is 700-900 ℃, and the carbonization time is 0.5-2 h.|[0023] The invention further provides a method for producing the activated carbon by using the Hunan oil-tea camellia shells.|[0024] Furthermore, the aperture of the activated carbon is 3-4 nm.|[0025] The invention also provides application of the activated carbon in a super capacitor.|[0026] According to the invention, the preparation of high-quality supercapacitor active carbon is realized by using oil tea shells with rich resources as raw materials and by using technologies such as low-concentration dilute alkali pretreatment of the raw materials, microwave-assisted activation reaming and secondary reaming.|[0027] The principle of microwave heating is that polar substance molecules absorb electromagnetic energy in a microwave electromagnetic field to vibrate at a very high speed to generate heat energy. Therefore, the microwave heating has the characteristics of uniformity and rapidness. The invention pre-treats the Xiang camellia oleifera shells by microwave heating, which is beneficial to driving alkali (such as NaOH/KOH) to diffuse into the biological tissue cells and micropores of the Xiang camellia oleifera shells, and increasing the activity and reaction rate of components such as degraded lignin, cellulose and the like, thereby reducing the alkali concentration and shortening the treatment time and achieving the aim of producing the activated carbon; thereby being beneficial to protecting production equipment, reducing production cost and protecting environment.|[0028] When microwave heating is utilized for ash removal, activation and drying, as the heating object is heated from inside to outside in a three-dimensional simultaneous heating mode, water molecules are driven to be in the holes at the same time, particularly the hole diameters of micropores (the diameter is less than 2nm) are subjected to repeated diffusion movement to carry out secondary activation and hole expansion, the communication among multi-level holes is facilitated, the proportion of mesopores is obviously increased, the requirement of a super capacitor on the reasonable distribution of the hole diameters of the activated carbon material is met, and the electrochemical activity of the super capacitor is further increased. The ash removal refers to a process for removing non-carbon impurities in the activated carbon, and mainly removes metal substances in the activated carbon.|[0029] The temperature and time of microwave heating are the most important parameters for controlling the pore diameter of the activated carbon, if the temperature of microwave heating is too high or the heating time is too long, the pore diameter of the activated carbon is increased, and the performance of the activated carbon is affected by the excessively large pore diameter.|[0030] The method has the beneficial effects that the preparation of the activated carbon by using the Hunan oil tea shells can be realized by using the low-concentration alkali solution in combination with the microwave activation and ash removal technologies, the activated carbon has excellent performance, high mesopore proportion and high specific capacitance, and can be used in a super capacitor.|INVENTION MODE|[0031] Detailed Description|INVENTION MODE|[0032] Examples1|[0033] The method for preparing activated carbon by using Hunan oil tea shells provided by the embodiment comprises the following steps:|[0034] a. drying Xiang oil tea fruit shell at 250 deg.C, crushing to certain particle size, and sieving with 20 mesh sieve.|[0035] b. Dipping 20-mesh Hunan oil-tea camellia fruit shell powder and 2% KOH according to the mass ratio of 1:4, wherein the temperature is 70 ℃, and the time is 24 hours.|[0036] c. And (3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 200 ℃, and the time is 2 hours.|[0037] d. Carbonizing the once activated Hunan oil-tea camellia fruit shell powder by using a carbonization furnace at 700 ℃ for 2 hours; and crushing by a double-roller machine, and further crushing by a ball mill to obtain carbon powder with the particle size range of 4-7 mu m.|[0038] e. The carbon powder is subjected to microwave heating and ash removal by using hydrochloric acid with the concentration of 0.5 percent at the temperature of 450 ℃ for 0.5h, and then is filtered and washed to be neutral by using high-purity water.|[0039] f. And adding ultrapure water with the same mass as the carbon powder, heating to 450 ℃ by using microwave, and performing secondary activation for 0.5h until the activated carbon product is dried to obtain the activated carbon product.|[0040] The specific surface area of the activated carbon is 1268m by detection2(iv)/g, iodine adsorption value of 560.60mg/g, methylene blue adsorption value of 450.58mg/g, density of 0.45g/mL, average pore diameter of 3.8nm, pH =6, specific capacitance of the capacitor of 268F/g.|INVENTION MODE|[0041] Examples2|[0042] The method for preparing activated carbon by using Hunan oil tea shells provided by the embodiment comprises the following steps:|[0043] a. drying Xiang oil tea fruit shell at 250 deg.C, crushing to certain particle size, and sieving with 50 mesh sieve.|[0044] b. Dipping 50-mesh Hunan oil-tea camellia fruit shell powder and 3% KOH according to the mass ratio of 1:1, wherein the temperature is 90 ℃, and the time is 7 hours.|[0045] c. And (3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 450 ℃, and the time is 0.5 h.|[0046] d. Carbonizing the once activated Hunan oil-tea camellia fruit shell powder by using a carbonization furnace at 900 ℃ for 0.5 h; and crushing by a double-roller machine, and further crushing by a ball mill to obtain carbon powder with the particle size range of 4-8 mu m.|[0047] e. The carbon powder is subjected to microwave heating and ash removal by using hydrochloric acid with the concentration of 2 percent at the temperature of 200 ℃ for 1 hour, and then is filtered and washed to be neutral by using high-purity water.|[0048] f. And adding ultrapure water with the mass 3 times that of the carbon powder, and carrying out secondary activation by microwave heating at the temperature of 450 ℃ until the activated carbon is dried to obtain an activated carbon product. .|[0049] The specific surface area of the activated carbon is 1310m by detection2The specific capacitance of the capacitor is 256F/g, the iodine adsorption value is 479.60mg/g, the methylene blue adsorption value is 419.70mg/g, the density is 0.42g/ml, the average pore diameter is 3.3nm, the pH = 8.|INVENTION MODE|[0050] Examples3|[0051] The method for preparing activated carbon by using Hunan oil tea shells provided by the embodiment comprises the following steps:|[0052] a. drying Xiang oil tea fruit shell at 250 deg.C, crushing to certain particle size, and sieving with 100 mesh sieve.|[0053] b. Dipping 100-mesh Hunan oil-tea camellia fruit shell powder and 5% KOH in a mass ratio of 1:2 at the temperature of 80 ℃ for 18 h.|[0054] c. And (3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 200 ℃, and the time is 1 h.|[0055] d. Carbonizing the raw material subjected to primary activation by using a carbonization furnace at 700 ℃ for 1.5 h; and crushing by a double-roller machine, and further crushing by a ball mill to obtain carbon powder with the particle size range of 4-7 mu m.|[0056] e. The carbon powder is subjected to microwave heating and ash removal by using hydrochloric acid with the concentration of 0.5 percent at the temperature of 450 ℃ for 1 hour, and then filtered and washed to be neutral by using high-purity water.|[0057] f. And adding ultrapure water with the mass 2 times that of the carbon powder, heating to 300 ℃ by using microwave, carrying out secondary activation, and continuing heating by using microwave until the activated carbon is dried to obtain an activated carbon product.|[0058] The specific surface area of the activated carbon is 1258m by detection2(iv)/g, iodine adsorption value of 529.60mg/g, methylene blue adsorption value of 453.58mg/g, density of 0.45g/ml, average pore diameter of 3.2nm, pH =6, and capacitance of capacitor of 232F/g. (CN104803381)|TECHNICAL FIELD|[0002] The invention relates to a method for preparing activated carbon by using Hunan oil tea shells, the activated carbon and application thereof, and belongs to the field of biochemical engineering.|BACKGROUND ART|[0004] Energy and environmental problems are important problems facing the world and are in a trend of increasing severity, and thus, countries are forced to search new energy and new energy conversion and storage modes. The super capacitor is used as a storage and conversion mode of energy, and has the advantages of high charging speed, high power, long service life and the like, so that the super capacitor is widely applied to electronic products (a coordinator and a computer storage), and is also beginning to be applied to energy supplement and recovery of electric automobiles, cranes, subways and the like. Activated carbon was the earliest electrode material used in supercapacitors and is the only carbon material for double layer capacitors currently commercialized. The performance and price of activated carbon become key factors that restrict the development and application of supercapacitors.|[0005] The active carbon is mainly derived from three kinds, including biomass active carbon (fruit shell, tree, etc.), coal active carbon, and resin active carbon. The quality of coal-based activated carbon is influenced by the quality of coal, and particularly, the development of the coal-based activated carbon is restricted by the characteristics of limited resources and non-renewable resources. The resin activated carbon has stable performance, but the resin preparation technology is complex and the price is expensive. The method for preparing the activated carbon by using the biomass as the raw material has the advantages of rich and reproducible resources, meets the requirement of low-carbon social development, and gradually becomes a hotspot of research and development of people. Particularly, the fruit shell is used as a byproduct of agriculture, has extremely rich resources and a natural pore structure, and is a high-quality raw material for preparing the active carbon. However, the existing patent technology for preparing the super-capacitor activated carbon has the problems of large acid or alkali consumption and the like, for example, the acid concentration is up to 72% when the super-capacitor activated carbon is prepared by Chinese patent (CN 102205963A), and the mass ratio of the alkali carbon is up to 5:1 when the super-capacitor activated carbon is prepared by Chinese patent (CN 103539114A), so that the acid and alkali substances with high proportion are not only strong in corrosivity and easy to cause environmental pollution, but also directly cause higher production cost. Currently, coconut shells, almond shells and the like are used as main sources of supercapacitor active carbon, but the materials are influenced by climate reasons in China, and have strong regional resource distribution and limited sources.|[0006] The camellia oleifera shells are byproducts of camellia oleifera seeds after kernels are separated, the camellia oleifera is a special woody oil crop in China and mainly distributed in Hunan, Hubei, Guangdong, Guangxi, Fujian, Jiangxi and other provinces, the Hunan camellia oleifera shells are the camellia oleifera shells in the Hunan, and the area of the existing camellia oleifera in China is about 400 x 104hm2Annual oil tea fruit nearly 560 x 104t. In recent years, the development of the oil tea industry is vigorously promoted by China, and the yield of oil tea steadily increases year by year. The Hunan oil-tea camellia shells account for 60 percent of the weight of the oil-tea camellia fruits, and the resources are extremely rich. At present, most of Hunan oil tea shells are scattered in the hands of farmers, are basically used as fuels for baking in winter, have low added value and pollute the environment.|[0007] The Hunan oil tea fruit shell mainly comprises lignin, cellulose and the like, and is a high-quality raw material for preparing the activated carbon. With the enhancement of consciousness on resource utilization, people begin to use Hunan oil-tea camellia shells to prepare activated carbon for adsorption (a, Lijiaxing and the like, agricultural product processing (academic journal), 2013,10:20-24, b, horsepower and the like, grain and food industry, 2009,16(3):19-21, c, Longliujin and the like, Guangxi university report: Nature science edition, 2012,37(3):425 + 429), but the prepared activated carbon has poor quality and can only be used as an industrial adsorbent. Chinese patents (CN 102502628A, CN 103011155A) all adopt high-concentration phosphoric acid (80%) to treat Xiang tea-oil tree shells to prepare activated carbon for adsorption; chinese patent (CN 103030710A) adopts high-concentration zinc chloride (50%) or high-alkali carbon ratio (4:1) to process Xiang oil tea fruit shell to prepare activated carbon for adsorption. The technologies use high-concentration acid or high alkali-carbon ratio, belong to the traditional activated carbon preparation process, and have the problems of high cost, serious environmental pollution, low product quality and the like.|DISCLOSURE|[0008] Disclosure of Invention|[0009] The invention solves the technical problems of reducing the production cost of preparing the activated carbon by using Hunan oil-tea camellia shells and improving the product quality of the activated carbon.|[0010] The technical scheme of the invention is to provide a method for preparing activated carbon by using Hunan oil tea shells, which comprises the following steps:|[0011] (1) drying, crushing and sieving Hunan oil-tea camellia shells to obtain Hunan oil-tea camellia shell powder;|[0012] (2) dipping the Xiang oil tea fruit shell powder by using an alkali solution;|[0013] (3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 200-450 ℃, and the time is 0.5-2 h;|[0014] (4) carbonizing the once activated Xiang oil tea fruit shell powder, and crushing to obtain carbon powder;|[0015] (5) adding a strong acid solution into the carbon powder, performing microwave heating for ash removal at the temperature of 200-450 ℃ for 0.5-1 h, and washing the carbon powder to be neutral by using water after ash removal;|[0016] (6) adding water with the mass being 1-5 times that of the carbon powder into the washed carbon powder, and performing secondary activation by using microwaves until the carbon powder is dried to obtain activated carbon, wherein the temperature of the secondary activation is 200-450 ℃.|[0017] Further, the alkali solution is 2-5 wt% of NaOH or KOH solution.|[0018] Further, the dipping temperature is 70-90 ℃ and the time is 7-24 h.|[0019] Further, in the step (1), the grain size of the Hunan oil-tea camellia fruit shell powder is 20-100 meshes.|[0020] Further, the particle size of the carbon powder is 4-8 mu m.|[0021] Further, the strong acid solution is 0.5-5 wt% of HCl or H2SO4And (3) solution.|[0022] Further, the carbonization temperature is 700-900 ℃, and the carbonization time is 0.5-2 h.|[0023] The invention further provides a method for producing the activated carbon by using the Hunan oil-tea camellia shells.|[0024] Furthermore, the aperture of the activated carbon is 3-4 nm.|[0025] The invention also provides application of the activated carbon in a super capacitor.|[0026] According to the invention, the preparation of high-quality supercapacitor active carbon is realized by using oil tea shells with rich resources as raw materials and by using technologies such as low-concentration dilute alkali pretreatment of the raw materials, microwave-assisted activation reaming and secondary reaming.|[0027] The principle of microwave heating is that polar substance molecules absorb electromagnetic energy in a microwave electromagnetic field to vibrate at a very high speed to generate heat energy. Therefore, the microwave heating has the characteristics of uniformity and rapidness. The invention pre-treats the Xiang camellia oleifera shells by microwave heating, which is beneficial to driving alkali (such as NaOH/KOH) to diffuse into the biological tissue cells and micropores of the Xiang camellia oleifera shells, and increasing the activity and reaction rate of components such as degraded lignin, cellulose and the like, thereby reducing the alkali concentration and shortening the treatment time and achieving the aim of producing the activated carbon; thereby being beneficial to protecting production equipment, reducing production cost and protecting environment.|[0028] When microwave heating is utilized for ash removal, activation and drying, as the heating object is heated from inside to outside in a three-dimensional simultaneous heating mode, water molecules are driven to be in the holes at the same time, particularly the hole diameters of micropores (the diameter is less than 2nm) are subjected to repeated diffusion movement to carry out secondary activation and hole expansion, the communication among multi-level holes is facilitated, the proportion of mesopores is obviously increased, the requirement of a super capacitor on the reasonable distribution of the hole diameters of the activated carbon material is met, and the electrochemical activity of the super capacitor is further increased. The ash removal refers to a process for removing non-carbon impurities in the activated carbon, and mainly removes metal substances in the activated carbon.|[0029] The temperature and time of microwave heating are the most important parameters for controlling the pore diameter of the activated carbon, if the temperature of microwave heating is too high or the heating time is too long, the pore diameter of the activated carbon is increased, and the performance of the activated carbon is affected by the excessively large pore diameter.|[0030] The method has the beneficial effects that the preparation of the activated carbon by using the Hunan oil tea shells can be realized by using the low-concentration alkali solution in combination with the microwave activation and ash removal technologies, the activated carbon has excellent performance, high mesopore proportion and high specific capacitance, and can be used in a super capacitor.|INVENTION MODE|[0031] Detailed Description|INVENTION MODE|[0032] Examples1|[0033] The method for preparing activated carbon by using Hunan oil tea shells provided by the embodiment comprises the following steps:|[0034] a. drying Xiang oil tea fruit shell at 250 deg.C, crushing to certain particle size, and sieving with 20 mesh sieve.|[0035] b. Dipping 20-mesh Hunan oil-tea camellia fruit shell powder and 2% KOH according to the mass ratio of 1:4, wherein the temperature is 70 ℃, and the time is 24 hours.|[0036] c. And (3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 200 ℃, and the time is 2 hours.|[0037] d. Carbonizing the once activated Hunan oil-tea camellia fruit shell powder by using a carbonization furnace at 700 ℃ for 2 hours; and crushing by a double-roller machine, and further crushing by a ball mill to obtain carbon powder with the particle size range of 4-7 mu m.|[0038] e. The carbon powder is subjected to microwave heating and ash removal by using hydrochloric acid with the concentration of 0.5 percent at the temperature of 450 ℃ for 0.5h, and then is filtered and washed to be neutral by using high-purity water.|[0039] f. And adding ultrapure water with the same mass as the carbon powder, heating to 450 ℃ by using microwave, and performing secondary activation for 0.5h until the activated carbon product is dried to obtain the activated carbon product.|[0040] The specific surface area of the activated carbon is 1268m by detection2(iv)/g, iodine adsorption value of 560.60mg/g, methylene blue adsorption value of 450.58mg/g, density of 0.45g/mL, average pore diameter of 3.8nm, pH =6, specific capacitance of the capacitor of 268F/g.|INVENTION MODE|[0041] Examples2|[0042] The method for preparing activated carbon by using Hunan oil tea shells provided by the embodiment comprises the following steps:|[0043] a. drying Xiang oil tea fruit shell at 250 deg.C, crushing to certain particle size, and sieving with 50 mesh sieve.|[0044] b. Dipping 50-mesh Hunan oil-tea camellia fruit shell powder and 3% KOH according to the mass ratio of 1:1, wherein the temperature is 90 ℃, and the time is 7 hours.|[0045] c. And (3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 450 ℃, and the time is 0.5 h.|[0046] d. Carbonizing the once activated Hunan oil-tea camellia fruit shell powder by using a carbonization furnace at 900 ℃ for 0.5 h; and crushing by a double-roller machine, and further crushing by a ball mill to obtain carbon powder with the particle size range of 4-8 mu m.|[0047] e. The carbon powder is subjected to microwave heating and ash removal by using hydrochloric acid with the concentration of 2 percent at the temperature of 200 ℃ for 1 hour, and then is filtered and washed to be neutral by using high-purity water.|[0048] f. And adding ultrapure water with the mass 3 times that of the carbon powder, and carrying out secondary activation by microwave heating at the temperature of 450 ℃ until the activated carbon is dried to obtain an activated carbon product. .|[0049] The specific surface area of the activated carbon is 1310m by detection2The specific capacitance of the capacitor is 256F/g, the iodine adsorption value is 479.60mg/g, the methylene blue adsorption value is 419.70mg/g, the density is 0.42g/ml, the average pore diameter is 3.3nm, the pH = 8.|INVENTION MODE|[0050] Examples3|[0051] The method for preparing activated carbon by using Hunan oil tea shells provided by the embodiment comprises the following steps:|[0052] a. drying Xiang oil tea fruit shell at 250 deg.C, crushing to certain particle size, and sieving with 100 mesh sieve.|[0053] b. Dipping 100-mesh Hunan oil-tea camellia fruit shell powder and 5% KOH in a mass ratio of 1:2 at the temperature of 80 ℃ for 18 h.|[0054] c. And (3) performing primary activation on the dipped Hunan oil-tea camellia fruit shell powder by using microwaves, wherein the temperature of the primary activation is 200 ℃, and the time is 1 h.|[0055] d. Carbonizing the raw material subjected to primary activation by using a carbonization furnace at 700 ℃ for 1.5 h; and crushing by a double-roller machine, and further crushing by a ball mill to obtain carbon powder with the particle size range of 4-7 mu m.|[0056] e. The carbon powder is subjected to microwave heating and ash removal by using hydrochloric acid with the concentration of 0.5 percent at the temperature of 450 ℃ for 1 hour, and then filtered and washed to be neutral by using high-purity water.|[0057] f. And adding ultrapure water with the mass 2 times that of the carbon powder, heating to 300 ℃ by using microwave, carrying out secondary activation, and continuing heating by using microwave until the activated carbon is dried to obtain an activated carbon product.|[0058] The specific surface area of the activated carbon is 1258m by detection2(iv)/g, iodine adsorption value of 529.60mg/g, methylene blue adsorption value of 453.58mg/g, density of 0.45g/ml, average pore diameter of 3.2nm, pH =6, and capacitance of capacitor of 232F/g. Family Number|(70372919)|70372919|Abstract|(CN104803381B B)|The invention relates to a method for preparing activated carbon from Hunan camellia oleifera shells , activated carbon and an application of the activated carbon , and belongs to the field of biochemical engineering . The method comprises the following steps : the Hunan camellia oleifera shells are dried , crushed and sieved ; Hunan camellia oleifera shell powder is dipped with aqueous alkali ; the dipped Hunan camellia oleifera shell powder is subjected to primary activation with microwaves , the temperature for the primary activation is 200-450 DEG C , and the primary activation is performed for 0.5-2 h ; the Hunan camellia oleifera shell powder after the primary activation is carbonized and ground to obtain powdered carbon ; a strong acid solution is added to the powdered carbon , ash removal is performed through microwave heating at the temperature of 200-450 DEG C for 0.5-1 h , and the powdered carbon after ash removal is washed to neutral ; 1-5 times of mass of water is added to the powdered carbon after washing , the mixture is subjected to secondary activation with microwaves until the mixture is dried , then the activated carbon is obtained , and the temperature for the secondary activation is 200-450 DEG C . The activated carbon prepared with the method is applicable to a supercapacitor . |IPC codes|(CN104803381B B)|C01B - 031/12 | Electrical machinery, apparatus, energy|Environmental technology|Materials, metallurgy Y02E-060/13 Y02E-060/13 B09B-003/00|C01B-031/12|H01G-011/44 B09B-003/00|C01B-031/12|H01G-011/44 CN117142469|CN116715218|CN112357920|CN106276899|CN112408390|CN110902677|CN110010358B|CN106047508|CN118637600B CN117142469 107590936 WHO=Examiner SELF=N CAT=Y|CN116715218 106425601 WHO=Examiner SELF=N CAT=Y|CN112357920 92736928 WHO=Examiner SELF=N CAT=Y|CN106276899 75068650 WHO=Examiner SELF=N CAT=Y|CN112408390 92903337 WHO=Examiner SELF=N CAT=A|CN110902677 87969257 WHO=Examiner SELF=N CAT=A|CN110010358B 85333193 WHO=Examiner SELF=N CAT=A|CN106047508 74469588 WHO=Examiner SELF=N CAT=A|CN118637600B 111439982 WHO=Examiner SELF=N CN103435039|US20140161709|CN102205960|JP4266711 CN103435039 59418845 WHO=Examiner SELF=N CAT=A|US20140161709 66203140 WHO=Examiner SELF=N CAT=A|CN102205960 7435796 WHO=Examiner SELF=N CAT=A|JP4266711 22438889 WHO=Examiner SELF=N CAT=A US20140161709; CN103435039; JP4266711; CN102205960 GRANTED (CN104803381)|GRANTED ALIVE (CN104803381)|ALIVE (CN104803381)|LEGAL DETAILS FOR CN104803381|Actual or expected expiration date=2035-03-25|Legal state=ALIVE|Status=GRANTED|Event publication date=2015-03-25|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN201510132681|Application date=2015-03-25|Standardized application number=2015CN-0132681|Event publication date=2015-07-29|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN104803381|Publication stage code=A|Publication date=2015-07-29|Standardized publication number=CN104803381|Event publication date=2015-07-29|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2015-08-26|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2016-08-17|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN104803381|Publication stage code=B|Publication date=2016-08-17|Standardized publication number=CN104803381B|Event publication date=2016-08-17|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right|Event publication date=2020-07-10|Event code=CN/PD01|Event group=Restitution or restoration Opposition and reexamination events|Discharge of preservation hold on patent right|Effective date of the event=2020-05-12|Event publication date=2020-07-10|Event code=CN/PP01|Event indicator=Pos|Event group=Restitution or restoration Opposition and reexamination events|Preservation and discharge of patent right|Effective date of the event=2020-05-12 (CN104803381)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjlYBtpEL2VnGBj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=SCDIdRyXHSvJDxPt6Gqr%252FbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN104803381)|CN (CN104803381)|NAME=Changsha Guo Rong new forms of energy Co., Ltd , COUNTRY=CN (CN104803381)|NAME=LU HONG;CHANGSHA ZONEKEY PATENT LAW FIRM , REG=43113|(CN104803381)|NAME=LU HONG;CHANGSHA ZONEKEY PATENT LAW FIRM (CN104803381)|NAME=XieRong An|NAME=Liu Dengyou|NAME=Li Zhiguang|NAME=Zhou Zhi|NAME=DONG XINRONG|NAME=Lin Zhongfu|NAME=Wang Guoqing|NAME=SONG YUNFENG|NAME=Kuang Hao|NAME=WU LIJUN|(CN104803381)|NAME=XIE RONGAN|NAME=LIU DENGYOU|NAME=LI ZHIGUANG|NAME=ZHOU ZHI|NAME=DONG XINRONG|NAME=LIN ZHONGFU|NAME=WANG GUOQING|NAME=SONG YUNFENG|NAME=KUANG HAO|NAME=WU LIJUN 0 1 Titre: (CN104803381)|Method for preparing activated carbon from Hunan oil tea shells, activated carbon and application of activated carbon Résumé: (CN104803381)|The invention relates to a method for preparing activated carbon from Hunan camellia oleifera shells, activated carbon and an application of the activated carbon, and belongs to the field of biochemical engineering. The method comprises the following steps: the Hunan camellia oleifera shells are dried, crushed and sieved; Hunan camellia oleifera shell powder is dipped with aqueous alkali; the dipped Hunan camellia oleifera shell powder is subjected to primary activation with microwaves, the temperature for the primary activation is 200-450 DEG C, and the primary activation is performed for 0.5-2 h; the Hunan camellia oleifera shell powder after the primary activation is carbonized and ground to obtain powdered carbon; a strong acid solution is added to the powdered carbon, ash removal is performed through microwave heating at the temperature of 200-450 DEG C for 0.5-1 h, and the powdered carbon after ash removal is washed to neutral; 1-5 times of mass of water is added to the powdered carbon after washing, the mixture is subjected to secondary activation with microwaves until the mixture is dried, then the activated carbon is obtained, and the temperature for the secondary activation is 200-450 DEG C. The activated carbon prepared with the method is applicable to a supercapacitor. 124 Abstract gpt-4o-mini no The article focuses on the preparation and application of activated carbon from oil tea shells, which does not relate to accelerated weathering or CO₂ capture.
125 CN202210611205 CN202210611205 CN114887351|CN114887351 101303669 CN114887351 B 2023-04-28 [CN114887351B]|CN114887351 A 2022-08-12 [CN114887351] 2022-05-31 2022-05-31 2023-04-28|2022-08-12 (CN114887351B)|2023-04-28 (CN114887351)|2042-05-31 (CN114887351)|System and method for supercritical carbon dioxide extraction of green corrosion inhibitor for carbon capture and sequestration (CN114887351)|The invention discloses a supercritical carbon dioxide extraction green corrosion inhibitor system and method, and belongs to the technical field of carbon capture and storage and supercritical fluid extraction, and the method comprises the following steps: extracting part of carbon dioxide from a carbon capture side, purifying, liquefying, uniformly mixing with an entrainer, feeding into a high-pressure pump and a heat exchanger, converting into a supercritical extraction agent, an extraction raw material enters a continuous extraction device after being subjected to fine screening, slicing, drying and crushing, an entrainer is separated after the green corrosion inhibitor obtained through extraction passes through a rectifying tower, the entrainer is injected into a carbon capture side to-be-transported supercritical carbon dioxide, whether effective components of the corrosion inhibitor are separated or not is selected according to requirements, and carbon dioxide can be completely separated and obtained only by changing pressure and temperature during separation. The whole technological process is green and environment-friendly, energy is saved, the application scene of supercritical fluid extraction is further expanded, and the development of the carbon capture and storage technology is also promoted. XIAN JIAOTONG UNIVERSITY (CN114887351)|XI'AN JIAOTONG UNIVERSITY ([CN])|(CN114887351)|XI'AN JIAOTONG UNIVERSITY ([CN]) WANG YUESHE|TONG GUOHU|WANG XIAODAN|LI RUIDONG (CN114887351)|Wang Yueshe|Tong Guohu|Wang Xiaodan|Li Ruidong|(CN114887351)|WANG YUESHE|TONG GUOHU|WANG XIAODAN|LI RUIDONG (CN114887351)|FAN WEI;XI'AN TONG DA (TONG SHENG) PATENT & TRADEMARK AGENCY CO. LTD.|Reg. Nb: 61200 (CN114887351)|Compared with the conventional separation method, the supercritical carbon dioxide extraction technology does not use an organic solvent and has no solvent residue; heavy metal and pesticide residues are avoided; no waste gas, waste water and waste residue exists in the whole process; has the advantages of low extraction temperature, strong selectivity, high efficiency, low energy consumption, no pollution and the like.|Further, the pressure and temperature of the green corrosion inhibitor active ingredient when separating from the rectifying tower and the pressure and temperature when converting the carbon dioxide source to be transported from the carbon capturing side into supercritical carbon dioxide need to be far away from the critical pressure and critical temperature, and the green corrosion inhibitor active ingredient has the advantages that the green corrosion inhibitor active ingredient is easy to change drastically on one hand near the critical point; on the other hand, the large change of the supercritical fluid density near the critical point can cause the content of the contained effective corrosion inhibitor component to be reduced.|The soaking method is simple and convenient to operate, but has the problems of low efficiency, low extraction rate and the like; the heating reflux method and the Soxhlet extraction method have similar extraction principles and long extraction time, but the Soxhlet extraction method has the advantages of less solvent and high extraction efficiency; in addition, the Soxhlet extraction method has high extraction temperature, and the problem of temperature resistance of the plant extract should be considered; the enzyme activity in the enzymolysis method is related to temperature, pH, reactant concentration and the like, has extremely severe requirements on the extraction environment and has a narrow application range; the ultrasonic extraction method has high extraction efficiency, but the electric energy consumption is a main limiting factor.|Although certain requirements are imposed on the quality of the captured carbon dioxide gas, such as the water content, the hydrogen sulfide content, etc., in terms of design and health safety, etc., strict control is required, it is impossible to obtain completely pure carbon dioxide from the practical operation and economical point of view. However, the presence of these impurities can cause corrosion problems inside the pipe.| (CN114887351)|1. The system for extracting the green corrosion inhibitor by using the supercritical carbon dioxide for capturing and sealing the carbon is characterized by comprising an extraction raw material pretreatment module, a supercritical carbon dioxide extractant production module, a carbon dioxide transportation treatment module and a green corrosion inhibitor filling and separation module, wherein the extraction raw material pretreatment module, the supercritical carbon dioxide extractant production module, the carbon dioxide transportation treatment module and the green corrosion inhibitor filling and separation module are arranged between a carbon capturing side and a carbon sealing or utilizing side;the supercritical carbon dioxide extractant production module comprises a liquid carbon dioxide pretreatment unit, an extraction heat exchanger (08), an extraction backpressure valve (09) and a supercritical continuous extraction device (10) which are connected in sequence;the green corrosion inhibitor filling and separating module comprises a rectifying tower (13) and a green corrosion inhibitor separating unit, wherein the tail end of the carbon capturing side is introduced into the outlet end of the rectifying tower (13), the tail end of the carbon capturing side is connected with a carbon transportation side, the outlet of the carbon transportation side is connected with the green corrosion inhibitor separating unit, and the outlet of the green corrosion inhibitor separating unit is connected with a carbon sealing and storing and utilizing side;the extraction raw material pretreatment module is connected with an inlet of a supercritical continuous extraction device (10), and an outlet of the supercritical extraction device (10) is connected with an inlet of a rectifying tower (13);the outlet of the transported carbon dioxide treatment module and the outlet of the rectifying tower (13) are converged at a carbon transportation side;the carbon dioxide pretreatment unit comprises a purifier (02), a compressor (03), a condenser (04) and a liquid carbon dioxide storage tank (05) which are sequentially connected, wherein an outlet of the liquid carbon dioxide storage tank (05) is connected with a winding inlet at one end of a mixer (06), an entrainer storage tank (28) is connected with an entrainer auxiliary pump (29) and is connected with an inlet at the other end of the mixer (06), an outlet of the mixer (06) is connected with a high-pressure pump (07), and an outlet of the high-pressure pump (07) is connected with the extraction heat exchanger (08); the pressure of the compressor (03) is raised to 7.6-8.1 MPa, the temperature of the condenser (04) is lowered to room temperature, the pressure of the high-pressure pump (07) is raised to 7.4-40 MPa, and the temperature of the extraction heat exchanger (08) is raised to 35-80 ℃.| (CN114887351)|The invention also provides a method for extracting the green corrosion inhibitor by supercritical carbon dioxide, which comprises the following steps:|The invention discloses a supercritical carbon dioxide extraction green corrosion inhibitor system and a supercritical carbon dioxide extraction green corrosion inhibitor method, which belong to the technical field of carbon capture and sequestration and supercritical fluid extraction, and comprise the following steps: and (3) extracting part of carbon dioxide from the carbon capturing side, purifying and liquefying, mixing the carbon dioxide with an entrainer uniformly, sending the mixture into a high-pressure pump and a heat exchanger, converting the mixture into a supercritical extractant, carrying out fine screening, slicing, drying and crushing on an extracted raw material, then sending the extracted raw material into a continuous extraction device, separating the entrainer from the extracted green corrosion inhibitor after passing through a rectifying tower, injecting the entrainer into the carbon capturing side, and conveying the supercritical carbon dioxide to be separated, and selecting whether to separate the effective components of the corrosion inhibitor according to requirements, wherein the carbon dioxide can be completely separated by only changing the pressure and the temperature during separation.|the invention provides a system for supercritical carbon dioxide extraction green corrosion inhibitor for carbon capture and sequestration, which is characterized by comprising an extraction raw material pretreatment module, a supercritical carbon dioxide extractant production module, a carbon dioxide transportation treatment module, a green corrosion inhibitor filling and separating module and a carbon transportation side, wherein the extraction raw material pretreatment module, the supercritical carbon dioxide extractant production module, the carbon dioxide transportation treatment module, the green corrosion inhibitor filling and separating module and the carbon transportation side are arranged between a carbon capture side and a carbon sequestration or utilization side.| (CN114887351)|CARBON DIOXIDE(100,149)|CORROSION INHIBITOR(100,84)|CARBON CAPTURE(100,36)|GREEN CORROSION INHIBITOR(100,35)|SUPERCRITICAL CARBON DIOXIDE(100,35)|RECTIFYING TOWER(100,18)|CARBON DIOXIDE EXTRACTION(100,17)|SEQUESTRATION(100,12)|CARBON(100,2)|PRETREATMENT MODULE(79,11)|EXTRACTANT PRODUCTION MODULE(77,7)|SUPERCRITICAL EXTRACTANT(68,1)|TRANSPORTATION TREATMENT MODULE(67,5)|RECTIFYING TOWER OUTLET(62,1)|CORROSION INHIBITOR FILLING(60,10)|RECTIFYING TOWER INLET(60,1)|SUPERCRITICAL CONTINUOUS EXTRACTION(57,15)|SEPARATION MODULE(54,10)|EXTRACTION BACKPRESSURE VALVE(52,3)|CORROSION INHIBITOR SEPARATING(49,5)|CORROSION INHIBITOR ACTIVE INGREDIENT(48,11)|ENTRAINER ROD(43,1)|EXTRACTED GREEN CORROSION INHIBITOR(42,1)|ACTIVE INGREDIENT(39,11)|SUPERCRITICAL EXTRACTION(38,3)|EXTRACTION HEAT EXCHANGER(36,25)|ENTRAINER AUXILIARY PUMP(34,7)|CARBON DIOXIDE PRETREATMENT(34,6)|FINE SCREENING(34,1)|SOXHLET EXTRACTION(33,4)|CONVEYING CONDENSER(31,4)|WINDING INLET(31,1)|ULTRASONIC EXTRACTION(30,2)|CARBON SEALING(28,6)|ENTRAINER(28,6)|EXTRACTION ENVIRONMENT(27,1)|HEALTH SAFETY(27,1)|TREATMENT MODULE(26,1)|WASTE RESIDUE(26,1)|CARBON DIOXIDE ROD(24,2)|SOLVENT RESIDUE(24,1)|EXTRACTION TEMPERATURE(23,5)|TRANSPORT HEAT EXCHANGER(22,6)|CRUSHING(22,1)|EXTRACTING(22,1)|REAGENT(22,1)|RECTIFYING COLUMN(22,1)|ENZYMOLYSIS(21,2)|HEAT REFLUX(21,2)|CARBON DIOXIDE TREATMENT MODULE(21,1)|IMPURITY(21,1)|WASTEWATER(21,1)|ORGANIC SOLVENT(20,1)|EXTRACTION RAW MATERIAL(19,15)|ENTRAINER STORAGE TANK(19,3)|SUPERCRITICAL FLUID DENSITY(19,1)|TRANSPORTING CARBON(19,1)|CARBON TRANSPORTATION SIDE(18,9)|CONVEYING TREATMENT MODULE(18,2)|RECTIFYING TOWER TEMPERATURE(18,2)|SLICING(18,2)|SOAKING(18,2)|HYDROGEN SULFIDE CONTENT(18,1)|PULVERIZER(17,5)|CARBON DEVELOPMENT(17,1)|LIQUID CARBON DIOXIDE OUTLET(17,1)|PESTICIDE RESIDUE(17,1)|SAVE ENERGY(17,1)|PURIFIER(16,5)|EXTRACTION PRODUCT(16,4)|LIQUID CARBON DIOXIDE(15,10)|CONVEYING HEAT EXCHANGER(15,6)|CONDENSATION(15,3)|CONTAMINATION(15,2)|CONVEYING COMPRESSOR PRESSURE(15,2)|CORROSION(15,2)|EXTRACTING RAW MATERIAL(15,2)|STORAGE BIN(15,1)|COMPRESSOR(14,7)|ENZYME ACTIVITY(14,1)|SUPERCRITICAL FLUID EXTRACTION(13,6)|EXTRACTION RATE(13,3)|CORROSION INHIBITOR COMPONENT(13,2)|EXTRACTION HEAT EXCHANGER TEMPERATURE(13,2)|HYDROGEN SULFIDE(13,1)|PLANT EXTRACT(13,1)|METER(11,5)|SLICER(10,3)|CARBON TRANSPORTATION SIDE OUTLET(10,1)|STORAGE TANK(9,8)|DRYER(9,6)|CARBON SEQUESTRATION(9,5)|CARBON DIOXIDE GAS(9,3)|STRICT CONTROL(9,3)|WASTE HEAT RETURN(9,2)|DIVIDING WALL HEAT EXCHANGER(9,1)|LIMITING FACTOR(9,1)|SUPERCRITICAL RECTIFYING TOWER(9,1)|WASTE GAS(9,1)|HEAT EXCHANGER(8,4)|AWAY ROD(8,3)|APPLICATION SCENE(8,1)|CARBON DIOXIDE SOURCE(7,6)|TRANSPORT COMPRESSOR(7,3)|TRANSPORT CONDENSER(7,3)|CRITICAL POINT(7,2)|EXTRACTION KETTLE(7,2)|CARBON DIOXIDE NEED(7,1)|SUPERCRITICAL RECTIFICATION COLUMN(7,1)|ROOM TEMPERATURE(6,5)|CRITICAL PRESSURE(6,4)|CRITICAL TEMPERATURE(6,4)|ENERGY CONSUMPTION(6,3)|CARBON DIOXIDE TRANSPORTATION PIPELINE(6,2)|NATURAL GREEN CORROSION INHIBITOR(6,2)|OUTLET PIPELINE(6,2)|S01 CARBON DIOXIDE(6,2)|S03 CARBON DIOXIDE(6,2)|ELECTRIC ENERGY CONSUMPTION(6,1)|INHIBITING PIPELINE CORROSION(6,1)|LARGE CHANGE(6,1)|MULTIKETTLE EXTRACTION(6,1)|TAIL END(5,4)|TRANSPORTATION HEAT EXCHANGER(5,4)|UTILIZATION SIDE(5,2)|WATER CONTENT(5,2)|CARRYING OUT FINE SCREENING(5,1)|CONVEYING PIPELINE(5,1)|ECOLOGICAL ENVIRONMENT SUSTAINABLE DEVELOPMENT(5,1)|HEAVY METAL(5,1)|MICROWAVE EXTRACTION(5,1)|NONEXCLUSIVE INCLUSION(5,1)|OBTAINING HEAT SOURCE(5,1)|ORGANIC CORROSION INHIBITOR HARM(5,1)|PLANT CORROSION INHIBITOR EXTRACTION(5,1)|TEMPERATURE RESISTANCE(5,1)|TRANSPORTATION PIPELINE STANDARD(5,1)|CARBON DIOXIDE STREAM(4,6)|GASEOUS CARBON DIOXIDE(4,3)|CARBON COMPLEMENT SIDE(4,2)|CARBON TRAPPING(4,2)|SOLUTE CONTENT(4,2)|TECHNICAL DIFFICULTY(4,2)|TECHNICAL IDEA(4,2)|CAPTURE LINK(4,1)|EARLY DOMESTIC RELATED RESEARCHER(4,1)|GEOLOGICAL ENVIRONMENT(4,1)|GEOLOGICAL SEQUESTRATION AREA(4,1)|HARMFUL CORROSION INHIBITOR(4,1)|HEAT CONVEYING EXCHANGER(4,1)|INSUFFICIENT EXTRACTION(4,1)|LONG EXTRACTION TIME(4,1)|MAGAZINE CHAIN FEEDING(4,1)|NARROW APPLICATION RANGE(4,1)|SEPARATION METHOD(4,1)|CARBON CAPTURE SIDE(3,9)|CARBON DIOXIDE FLUID(3,4)|PLUG SIDE(3,3)|SHELL SIDE(3,3)|CORROSION INHIBITION COMPONENT(3,2)|EXTRACTANT(3,2)|ACTIVE INGREDIENT EXTRACT(3,1)|CORROSION INHIBITOR SEPARATION(3,1)|DAMAGING INSECT(3,1)|DISCHARGE EXTRACTION(3,1)|EXTRACTION SOLVENT ROD(3,1)|EXTRACTOR(3,1)|HUGE ECONOMIC LOSS(3,1)|IMPURITY CONTENT(3,1)|LIQUID ENTRAINER(3,1)|PORT CONTINUOUS EXTRACTION(3,1)|REMOVING IMPURITY(3,1)|ROD NATURAL PLANT(3,1)|ROD REED(3,1)|SEPARATION OUTLET(3,1)|SPHERICAL FEEDING(3,1)|SUBSTANCE EXTRACTION(3,1)|TUBULAR CONTINUOUS EXTRACTION(3,1)|MIXER(2,3)|ABSORBENT(2,1)|ALKALOID(2,1)|CAPTURED CARBON DIOXIDE(2,1)||(CN114887351)|CARBON DIOXIDE(100,161)|CORROSION INHIBITOR(100,82)|SUPERCRITICAL CARBON DIOXIDE(100,47)|GREEN CORROSION INHIBITOR(100,43)|CARBON CAPTURE(100,30)|RECTIFYING TOWER(100,18)|SEQUESTRATION(100,17)|EXTRACTANT PRODUCTION MODULE(71,5)|PRETREATMENT MODULE(69,10)|SUPERCRITICAL CONTINUOUS EXTRACTION(61,16)|RECTIFYING TOWER INLET(60,1)|CORROSION INHIBITOR FILLING(52,9)|CORROSION INHIBITOR SEPARATING(49,5)|SEPARATION MODULE(48,9)|SUPERCRITICAL EXTRACTION(39,3)|ECOLOGICAL ENVIRONMENT SUSTAINABLE DEVELOPMENT(39,1)|TRANSPORTATION TREATMENT MODULE(39,1)|ENTRAINER(37,7)|FINE SCREENING(34,1)|RECTIFICATION COLUMN(33,2)|ECOLOGICAL ENVIRONMENT(33,1)|EXTRACTION HEAT EXCHANGER(32,25)|TRANSPORTING COMPRESSOR(32,4)|CONVEYING PROCESSING MODULE(30,1)|CARBON DIOXIDE PRETREATMENT(29,6)|CARBON DIOXIDE EXTRACTION(27,8)|SUPERCRITICAL CONTINUOUS EXTRACTION PLANT(27,1)|CRUSHING(26,3)|WASTE RESIDUE(26,1)|EXTRACTION BACKPRESSURE VALVE(25,2)|ENTRAINER AUXILIARY PUMP(24,6)|SLICING(24,4)|SOLVENT RESIDUE(24,1)|CARBON DIOXIDE TRANSPORTATION(23,4)|TRANSPORTING CONDENSER(22,2)|EXTRACTING(22,1)|DRASTIC CHANGE(21,1)|FINISHING CARBON SEQUESTRATION(21,1)|IMPURITY(21,1)|WASTEWATER(21,1)|CARBON SEQUESTRATION(20,6)|ORGANIC SOLVENT(20,1)|EXTRACTION RAW MATERIAL(19,14)|SUPERCRITICAL FLUID DENSITY(19,1)|TRANSPORTING CARBON(19,1)|RECTIFYING TOWER TEMPERATURE(18,2)|CORROSION INHIBITOR COMPONENT(18,1)|EXTRACTION TEMPERATURE(17,5)|TRANSPORT CONDENSER(17,4)|TRANSPORTING HEAT EXCHANGER(17,4)|INDUSTRIAL REVOLUTION(17,1)|PESTICIDE RESIDUE(17,1)|SAVE ENERGY(17,1)|SUSTAINABLE DEVELOPMENT(17,1)|WORLD ECONOMY(17,1)|CORROSION INHIBITOR ACTIVE INGREDIENT(16,2)|CARBON SEALING(15,5)|EXTRACTION PRODUCT(15,5)|CONTAMINATION(15,2)|CORROSION(15,2)|CARBON CAPTURE DEVELOPMENT(15,1)|CARBON DIOXIDE CONTENT(15,1)|PRESSURE CHANGE(15,1)|CARBON TRANSPORTATION SIDE(14,11)|LIQUID CARBON DIOXIDE(13,13)|SUPERCRITICAL FLUID EXTRACTION(13,6)|TRANSPORT COMPRESSOR PRESSURE(13,2)|ENTRAINER STORAGE TANK(12,3)|POLAR ICE(12,1)|PURIFIER(11,5)|PULVERIZER(11,4)|STORAGE BIN(11,3)|SERIOUS DAMAGE(11,1)|SUPERCRITICAL CARBON DIOXIDE FLOW(11,1)|CONDENSATION(10,4)|DIVIDING WALL(10,3)|CARBON TRAPPING SIDE(10,1)|HEAT EXCHANGER(9,8)|UTILIZATION SIDE(9,3)|WASTE HEAT RETURN(9,2)|CARBON SIDE CONVEYER(9,1)|SUPERCRITICAL RECTIFYING TOWER(9,1)|WASTE GAS(9,1)|MIXER(8,4)|APPLICATION SCENE(8,1)|CARBON DIOXIDE SOURCE(7,6)|CRITICAL POINT(7,2)|EXTRACTION HEAT EXCHANGER TEMPERATURE(7,2)|EXTRACTION KETTLE(7,2)|ULTRASONIC EXTRACTION(7,2)|CARBON CAPTURE SIDE(6,23)|CRITICAL PRESSURE(6,4)|CRITICAL TEMPERATURE(6,4)|ENERGY CONSUMPTION(6,3)|METERING DEVICE(6,2)|NATURAL GREEN CORROSION INHIBITOR(6,2)|HEAVY METAL(6,1)|MULTIKETTLE EXTRACTION(6,1)|PIPELINE INHIBITING CORROSION(6,1)|RAW MATERIAL EXTRACTION(6,1)|SEA LEVEL(6,1)|SUPERCRITICAL RECTIFIER(6,1)|GASEOUS CARBON DIOXIDE(5,4)|SOXHLET EXTRACTION(5,4)|AWAY(5,3)|EXTRACTION BACK PRESSURE VALVE(5,3)|CARBON COMPLEMENTARY COLLECTION SIDE(5,1)|CREATIVE EFFORT(5,1)|GOLDEN CYPRESS(5,1)|INSUFFICIENT TRADITIONAL PLANT(5,1)|MAINSTREAM CORROSION INHIBITOR(5,1)|MICROWAVE EXTRACTION(5,1)|NONEXCLUSIVE INCLUSION(5,1)|ORGANIC CORROSION INHIBITOR HARM(5,1)|PLANT CORROSION INHIBITOR EXTRACTION(5,1)|SHELL SIDE(5,1)|ROOM TEMPERATURE(4,5)|DRYING MACHINE(4,3)|EXTRACTION RATE(4,3)|CARBON DIOXIDE CONVEYING PIPELINE(4,2)|ENZYMOLYSIS(4,2)|HEAT REFLUX(4,2)|SOLUTE CONTENT(4,2)|SUBSTANCE EXTRACTION(4,2)|TECHNICAL DIFFICULTY(4,2)|TECHNICAL IDEA(4,2)|TRANSPORT HEAT EXCHANGER PIPELINE(4,2)|CAPTURE LINK(4,1)|CONVEYING FEEDING CONTINUOUS EXTRACTION(4,1)|EXTRACTION RESIDUE(4,1)|GEOLOGICAL ENVIRONMENT(4,1)|GEOLOGICAL SEQUESTRATION AREA(4,1)|HARMFUL CORROSION INHIBITOR(4,1)|MAGAZINE CHAIN FEEDING(4,1)|QUICKLY DISSOLVED SOLUTE(4,1)|RECTIFYING COLUMN(4,1)|SEPARATION METHOD(4,1)|TOWER TEMPERATURE RECTIFICATION(4,1)|CARBON DIOXIDE GAS(3,5)|DRYER(3,3)|CORROSION INHIBITION COMPONENT(3,2)|EXTRACTANT(3,2)|SEPARATED GREEN CORROSION INHIBITOR(3,2)|SHELL PASS(3,2)|SOAKING(3,2)|ACTIVE INGREDIENT EXTRACT(3,1)|CARBON SUPPLEMENT(3,1)|CORROSION INHIBITOR SEPARATION(3,1)|DAMAGING INSECT(3,1)|DEEP OCEAN DEPTH(3,1)|EARLY RELATED RESEARCHER(3,1)|EXTRACTION ENVIRONMENT(3,1)|EXTRACTOR(3,1)|FAILURE RISK(3,1)|GREEN CORROSION INHIBITOR COMPONENT(3,1)|HEALTH SAFETY(3,1)|HUGE ECONOMIC LOSS(3,1)|IMPURITY CONTENT(3,1)|LIQUID ENTRAINER(3,1)|NATURAL PLANT(3,1)|PIPELINE STANDARD(3,1)|PORT CONTINUOUS EXTRACTION(3,1)|REMOVING IMPURITY(3,1)|SCREENING MACHINE(3,1)|SPHERICAL FEEDING(3,1)| (CN114887351)|1. The system for extracting the green corrosion inhibitor by using the supercritical carbon dioxide for capturing and sealing the carbon is characterized by comprising an extraction raw material pretreatment module, a supercritical carbon dioxide extractant production module, a carbon dioxide transportation treatment module and a green corrosion inhibitor filling and separation module, wherein the extraction raw material pretreatment module, the supercritical carbon dioxide extractant production module, the carbon dioxide transportation treatment module and the green corrosion inhibitor filling and separation module are arranged between a carbon capturing side and a carbon sealing or utilizing side;|the supercritical carbon dioxide extractant production module comprises a liquid carbon dioxide pretreatment unit, an extraction heat exchanger (08), an extraction backpressure valve (09) and a supercritical continuous extraction device (10) which are connected in sequence;|the green corrosion inhibitor filling and separating module comprises a rectifying tower (13) and a green corrosion inhibitor separating unit, wherein the tail end of the carbon capturing side is introduced into the outlet end of the rectifying tower (13), the tail end of the carbon capturing side is connected with a carbon transportation side, the outlet of the carbon transportation side is connected with the green corrosion inhibitor separating unit, and the outlet of the green corrosion inhibitor separating unit is connected with a carbon sealing and storing and utilizing side;|the extraction raw material pretreatment module is connected with an inlet of a supercritical continuous extraction device (10), and an outlet of the supercritical extraction device (10) is connected with an inlet of a rectifying tower (13);|the outlet of the transported carbon dioxide treatment module and the outlet of the rectifying tower (13) are converged at a carbon transportation side;|the carbon dioxide pretreatment unit comprises a purifier (02), a compressor (03), a condenser (04) and a liquid carbon dioxide storage tank (05) which are sequentially connected, wherein an outlet of the liquid carbon dioxide storage tank (05) is connected with a winding inlet at one end of a mixer (06), an entrainer storage tank (28) is connected with an entrainer auxiliary pump (29) and is connected with an inlet at the other end of the mixer (06), an outlet of the mixer (06) is connected with a high-pressure pump (07), and an outlet of the high-pressure pump (07) is connected with the extraction heat exchanger (08); the pressure of the compressor (03) is raised to 7.6-8.1 MPa, the temperature of the condenser (04) is lowered to room temperature, the pressure of the high-pressure pump (07) is raised to 7.4-40 MPa, and the temperature of the extraction heat exchanger (08) is raised to 35-80 ℃.|2. The system for supercritical carbon dioxide extraction green corrosion inhibitor for carbon capture and sequestration according to claim 1, characterized in that the rectification column (13) temperature is higher than the extraction temperature of the supercritical continuous extraction device (10); the pressure and the temperature of the rectifying tower (13) during separation are consistent with the pressure and the temperature of the carbon dioxide source to be transported from the carbon capturing side during conversion into supercritical carbon dioxide, and are far away from the critical pressure and the critical temperature.|3. The system for supercritical carbon dioxide extraction green corrosion inhibitor for carbon capture and sequestration according to claim 1, wherein the extraction raw material pretreatment module comprises a screening machine (30), an extraction raw material storage bin (31), a slicer (32), a dryer (33), a pulverizer (34) and a meter (35) connected in sequence, wherein the outlet of the meter (35) is connected to the supercritical continuous extraction device (10);|the carbon dioxide conveying treatment module comprises a conveying compressor (17), a conveying condenser (18), a conveying high-pressure pump (19) and a conveying heat exchanger (20) which are sequentially connected, wherein the inlet end of the conveying compressor (17) is connected with the carbon complement side through a pipeline, and the outlet end of the conveying heat exchanger (20) is connected with the green corrosion inhibitor filling and separating module through a pipeline.|4. A system for supercritical carbon dioxide extraction green corrosion inhibitor for carbon capture and sequestration according to claim 3, characterized in that the extraction heat exchanger (08), the transport heat exchanger (20) and the rectifying column (13) are all provided with pipes for obtaining heat sources on the carbon capture side, and the extraction heat exchanger (08) and the transport heat exchanger (20) are provided with pipes for returning waste heat to the carbon capture side.|5. A system for supercritical carbon dioxide extraction green corrosion inhibitor for carbon capture and sequestration according to claim 3, wherein the extraction heat exchanger (08) and the transport heat exchanger (20) are both a dividing wall heat exchanger, the heat flow into the extraction heat exchanger (08) and the transport heat exchanger (20) going through the shell side and the carbon dioxide going through the tube side.|6. The system for supercritical carbon dioxide extraction green corrosion inhibitor for carbon capture and sequestration according to claim 3, wherein the pulverizer (34) pulverizes the raw material powder to be extracted to a size of 80-150 mesh, and the meter (35) measures the content of the raw material powder to be extracted according to the supercritical carbon dioxide flow; the pressure of the conveying compressor (17) is increased to 7.6-8.1 MPa, the conveying condenser (18) is cooled to room temperature, and the pressure of the conveying high-pressure pump (19) is increased to 7.6-21 MPa.|7. The method for extracting green corrosion inhibitor by using the system for extracting green corrosion inhibitor by supercritical carbon dioxide for carbon capture and sequestration according to any one of claims 1 to 6, which is characterized by comprising the following steps:|s01, carbon dioxide generated by the carbon complement side is processed by the liquid carbon dioxide pretreatment unit to be changed into liquid carbon dioxide, and then enters an extraction heat exchanger (08) to be converted into supercritical carbon dioxide;|s02, the supercritical carbon dioxide in S01 enters a supercritical continuous extraction device (10) after the pressure is regulated by an extraction backpressure valve (09), and is extracted with natural products processed by the extraction raw material pretreatment module to generate extraction products, and the extraction products enter a rectifying tower (13), so that the green corrosion inhibitor active ingredients (15) are separated and are input to a carbon transportation side through a pipeline;|s03, carbon dioxide generated by the carbon capturing side is processed by a carbon dioxide transportation processing module to be changed into supercritical carbon dioxide, then the supercritical carbon dioxide is connected to the carbon transportation side, and is mixed with the green corrosion inhibitor active ingredient (15) in S02 to become supercritical carbon dioxide (21) to be transported after the green corrosion inhibitor is filled, and then carbon sealing or utilization is completed.|8. The method for supercritical carbon dioxide extraction of green corrosion inhibitor according to claim 7, wherein the natural product to be extracted contains green corrosion inhibitor active ingredient. (CN114887351)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of carbon trapping and sealing and supercritical fluid extraction corrosion inhibitors, and particularly relates to a system and a method for supercritical carbon dioxide extraction green corrosion inhibitor for carbon trapping and sealing.|BACKGROUND ART|[0002] Since the industrial revolution, the content of carbon dioxide in the atmosphere is remarkably improved, which directly causes the continuous rise of global surface temperature, the occurrence of disaster phenomena such as polar ice melting, sea level rising and the like, and serious damage is caused to the sustainable development of ecological environment and world economy. Carbon capture and sequestration technology (CCS) can separate and collect carbon dioxide from emission sources in a closed loop and transport a large amount to relevant areas for sequestration, and is a main means for slowing down climate change, and mainly consists of three links of capture, transportation and sequestration. The pipeline transportation technology is suitable for long-distance and large-output requirements. Carbon dioxide is generally transported in supercritical state from the viewpoints of economy and avoiding two-phase flow. Although certain requirements are imposed on the quality of the captured carbon dioxide gas, such as the water content, the hydrogen sulfide content, etc., in terms of design and health safety, etc., strict control is required, it is impossible to obtain completely pure carbon dioxide from the practical operation and economical point of view. However, the presence of these impurities can cause corrosion problems inside the pipe. The occurrence of corrosion in the supercritical carbon dioxide pipeline not only causes huge economic loss, but also brings about great potential safety hazard. The addition of a certain amount of corrosion inhibitor to the conveying pipeline is the most economical and effective corrosion control means at present, but part of the corrosion inhibitor such as chromate, mercury salt and the like is toxic, and other main flow corrosion inhibitors have different degrees and can have certain influence on the environment. The captured carbon dioxide will eventually be transported deep underground into long-term or permanently buried bodies such as oil and gas fields, salt water aquifers deposited in basins, coal seams, deep sea, and the like. It is rather a counter-operation if the harmful corrosion inhibitors are discharged into the geological environment in order to slow down the carbon dioxide pollution. Meanwhile, the corrosion inhibitor carried in the supercritical carbon dioxide pipeline is subjected to cleaning treatment at the conveying end, and the technical difficulty and the economic cost are huge.|[0003] The use of the natural green corrosion inhibitor can improve the conditions, and the natural green corrosion inhibitor has the characteristics of low toxicity and no pollution, and can reduce the harm of organic corrosion inhibitors and the like to human bodies and the environment in industrial production. Related studies have extracted effective components having corrosion inhibition effects from natural plants, marine plants and plant wastes for inhibiting pipeline corrosion. The plant corrosion inhibitor can be extracted from leaves, fruits, roots, seeds, etc. of plants. Early domestic related researchers extract corrosion inhibition effective components from reed and water lily leaves and stems and obtain good results, and then extract corrosion inhibition effective components in plants such as tea, pepper, pericarp, phellodendron and the like, so that corrosion inhibition effects with different degrees are obtained.|[0004] The extraction method of the plant corrosion inhibitor is various, and common extraction methods include a soaking method, a heating reflux method, a Soxhlet extraction method, an enzymolysis method, an ultrasonic extraction method, a microwave extraction method and the like. The soaking method is simple and convenient to operate, but has the problems of low efficiency, low extraction rate and the like; the heating reflux method and the Soxhlet extraction method have similar extraction principles and long extraction time, but the Soxhlet extraction method has the advantages of less solvent and high extraction efficiency; in addition, the Soxhlet extraction method has high extraction temperature, and the problem of temperature resistance of the plant extract should be considered; the enzyme activity in the enzymolysis method is related to temperature, pH, reactant concentration and the like, has extremely severe requirements on the extraction environment and has a narrow application range; the ultrasonic extraction method has high extraction efficiency, but the electric energy consumption is a main limiting factor.|[0005] Supercritical Fluid Extraction (SFE) is a new green separation technique and has been rapidly developed. The supercritical carbon dioxide extraction adopts carbon dioxide as a solvent, and carbon dioxide is used as a supercritical fluid, the critical temperature is 31.1 ℃, the critical pressure is 7.39MPa, the operation temperature and the operation pressure are easy to realize, and the energy consumption is low. The supercritical carbon dioxide fluid has high density and dielectric constant, has strong dissolving power to many substances, has a separation rate far faster than that of liquid extraction, and changes sharply along with the change of pressure and temperature, so that the supercritical carbon dioxide fluid has selectivity to the solubility of certain substances, and the solvent and the extract are easy to separate. Compared with the conventional separation method, the supercritical carbon dioxide extraction technology does not use an organic solvent and has no solvent residue; heavy metal and pesticide residues are avoided; no waste gas, waste water and waste residue exists in the whole process; has the advantages of low extraction temperature, strong selectivity, high efficiency, low energy consumption, no pollution and the like. Supercritical carbon dioxide extraction is currently mainly focused on plant essential oil, natural pigment, alkaloid (one of the effective components of traditional Chinese medicine) and the like.|[0006] Therefore, in order to solve the problems of internal corrosion in a supercritical carbon dioxide transportation pipeline, environmental hazard caused by the use of partial corrosion inhibitors, insufficient extraction methods of traditional plant corrosion inhibitors and the like, a green, environment-friendly, energy-saving and economic process method is needed.|DISCLOSURE|Disclosure of Invention|[0007] In order to overcome the defects and imperfections of the prior art, the invention aims to provide a system and a method for extracting a green corrosion inhibitor by supercritical carbon dioxide for carbon capture and sealing, which can solve the problems of corrosion in a supercritical carbon dioxide transportation pipeline and difficult extraction of a plant corrosion inhibitor, save energy consumption and reduce economic cost.|[0008] In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:|[0009] the invention provides a system for supercritical carbon dioxide extraction green corrosion inhibitor for carbon capture and sequestration, which is characterized by comprising an extraction raw material pretreatment module, a supercritical carbon dioxide extractant production module, a carbon dioxide transportation treatment module, a green corrosion inhibitor filling and separating module and a carbon transportation side, wherein the extraction raw material pretreatment module, the supercritical carbon dioxide extractant production module, the carbon dioxide transportation treatment module, the green corrosion inhibitor filling and separating module and the carbon transportation side are arranged between a carbon capture side and a carbon sequestration or utilization side.|[0010] The extraction raw material pretreatment module comprises a screening machine, a raw material storage bin to be extracted, a slicing machine, a dryer, a pulverizer and a meter.|[0011] The supercritical carbon dioxide extractant production module comprises a liquid carbon dioxide pretreatment unit, an extraction heat exchanger, an extraction backpressure valve and a supercritical continuous extraction device which are connected in sequence.|[0012] The liquid carbon dioxide pretreatment unit comprises a purifier, a compressor, a condenser and a liquid carbon dioxide storage tank which are sequentially connected, wherein the outlet end of the liquid carbon dioxide storage tank is connected with the inlet of one end of a mixer, the inlet of the other end of the mixer is connected with an entrainer auxiliary pump, the entrainer auxiliary pump is connected with the entrainer storage tank, the outlet end of the mixer is connected with the inlet end of a high-pressure pump, and the outlet end of the high-pressure pump is connected with an extraction heat exchanger.|[0013] And the inlet end at one side of the supercritical continuous extraction device is connected with the outlet end of the metering device of the extraction raw material pretreatment module, and the outlet end is connected with the rectifying tower of the green corrosion inhibitor filling and separating module.|[0014] The carbon dioxide conveying treatment module comprises a conveying compressor, a conveying condenser, a conveying high-pressure pump and a conveying heat exchanger which are sequentially connected, wherein the inlet end of the conveying compressor is connected with the carbon complement side through a pipeline, and the outlet end of the conveying heat exchanger is connected with the green corrosion inhibitor filling and separating module through a pipeline.|[0015] The green corrosion inhibitor filling and separating module comprises a rectifying tower and a green corrosion inhibitor separating unit, wherein the outlet end of the rectifying tower is introduced into the tail end of an outlet pipeline of the conveying heat exchanger, the tail end of the outlet pipeline of the conveying heat exchanger is connected to a carbon conveying side, and the outlet of the carbon conveying side is connected with the green corrosion inhibitor separating unit.|[0016] The green corrosion inhibitor separation unit comprises a heat exchange device and a separation device which are connected, wherein an outlet at one end of a carbon transportation side is directly connected with a carbon sealing or utilizing side, the other end of the carbon transportation side is connected with an inlet end of the heat exchange device, an outlet end of the heat exchange device is connected with the separation device, and an outlet of the separation device is connected with the carbon sealing or utilizing side.|[0017] Preferably, the entrainer auxiliary pump is a peristaltic pump; the supercritical continuous extraction device is a high-pressure extraction device for continuously feeding and discharging materials; the high-pressure pump and the high-pressure conveying pump are of plunger pump type, and particularly, a pump head sealing structure and a sealing material are required to be suitable for supercritical carbon dioxide fluid, and the sealing material such as graphite and oil-resistant rubber can face failure risks due to extremely strong extraction of the supercritical carbon dioxide fluid; the extraction heat exchanger and the transportation heat exchanger are of partition wall type, heat flow entering the extraction heat exchanger and the transportation heat exchanger passes through a shell side, and carbon dioxide passes through a tube side.|[0018] Preferably, the carbon capture side heat source is flue gas waste heat (more than or equal to 100 ℃) or circulating water waste heat (30-50 ℃).|[0019] Further preferably, the extraction heat exchanger, the transportation heat exchanger and the rectifying tower are all provided with pipelines for acquiring heat sources at the carbon capturing side, and the extraction heat exchanger and the transportation heat exchanger are provided with pipelines for returning waste heat to the carbon capturing side.|[0020] Further preferably, the purifier removes impurity gases, absorbents and moisture to meet the carbon dioxide standard for supercritical fluid extraction.|[0021] Further preferably, the size of the raw material powder to be extracted is 80-150 meshes.|[0022] Further preferably, the meter measures the raw material powder content to be extracted according to the supercritical carbon dioxide flow rate.|[0023] Supercritical carbon dioxide extraction has certain requirements on flow, and if the flow of carbon dioxide is increased, the mass transfer effect in the extraction process can be enhanced, and the solute which is rapidly dissolved is carried out from the raw material, so that the extraction time is shortened. Typically, the ratio of extract to carbon dioxide is about 1:20. The flow rate of the carbon dioxide is too fast, the residence time in the extraction kettle is shortened, the contact time with the extracted matter is shortened, and the solute content in the carbon dioxide is reduced. The flow rate of carbon dioxide is too slow, the residence time in the extraction kettle is prolonged, the contact time with the extracted substance is increased, the solute content in the carbon dioxide is increased, and the extraction time is prolonged.|[0024] Further preferably, the dryer requires strict control of the extraction feed moisture.|[0025] Further preferably, the pressure of the compressor is raised to 7.6Mpa to 8.1Mpa, and the temperature of the condenser is lowered to room temperature.|[0026] Further preferably, the pressure of the high-pressure pump is raised to 7.4Mpa to 40Mpa, and the temperature of the extraction heat exchanger is raised to 35 ℃ to 80 ℃.|[0027] Further preferably, the rectifying column temperature is higher than the extraction temperature of the supercritical continuous extraction device.|[0028] Further preferably, the pressure of the conveying compressor is increased to 7.6-8.1 Mpa, the conveying condenser is cooled to room temperature, and the pressure of the conveying high-pressure pump is increased to 7.6-21 Mpa.|[0029] The supercritical fluid extraction and supercritical carbon dioxide pipeline transportation are all gaseous carbon dioxide. There are two general schemes for converting gaseous carbon dioxide into supercritical carbon dioxide, one is to directly convert the gaseous carbon dioxide into supercritical carbon dioxide by a compressor, but a large volume of compressor is required for preparing the supercritical carbon dioxide, and a large temperature rise is generated in the isenthalpic compression process; and secondly, liquefying the carbon dioxide, and then obtaining the supercritical carbon dioxide by using a high-pressure pump. The invention adopts a second liquefaction scheme:|[0030] the invention adopts the scheme of liquefying at normal temperature and high pressure, even if gaseous carbon dioxide is converted into liquid state at normal temperature. When the temperature is 31.16 ℃ and the pressure is 7.6Mpa, the carbon dioxide starts to liquefy, and when the temperature in summer is high, the final pressure of the compressor can reach 8.1Mpa.|[0031] Preferably, the pressure and temperature of the green corrosion inhibitor active ingredient when separated from the rectifying tower are matched with the pressure and temperature when the carbon dioxide source to be transported from the carbon capturing side is converted into supercritical carbon dioxide, and the pressure and the temperature are far away from the critical pressure and the critical temperature. The values of the far-away range should be comprehensively considered, and the aspects of economy, safety and the like should be included, so that the far-away range is not suitable.|[0032] The invention also provides a method for extracting the green corrosion inhibitor by supercritical carbon dioxide, which comprises the following steps:|[0033] s01, carbon dioxide generated by the carbon complement side is processed by the liquid carbon dioxide pretreatment unit to be changed into liquid carbon dioxide, and then enters an extraction heat exchanger to be converted into supercritical carbon dioxide;|[0034] s02, the supercritical carbon dioxide enters a supercritical continuous extraction device after the pressure is regulated by an extraction back pressure valve, and is extracted with the natural product processed by the extraction raw material pretreatment module to generate an extraction product;|[0035] s03, carbon dioxide generated by the carbon capturing side is processed by a carbon dioxide transportation processing module to be changed into supercritical carbon dioxide, and then the supercritical carbon dioxide is connected to the carbon transportation side;|[0036] s04, the extracted product enters a rectifying tower to separate out the effective components of the green corrosion inhibitor, and the effective components are connected into the supercritical carbon dioxide of the S03, and carbon sealing and utilization are completed.|[0037] Preferably, the extracted natural product contains green corrosion inhibitor active ingredients.|[0038] Preferably, the carbon capture to-be-transported carbon dioxide source is from a typical carbon capture side, namely a large amount of carbon dioxide captured and collected by a coal-fired power plant, and the impurity content is required to meet the standard of a transportation pipeline.|[0039] Compared with the prior art, the invention has the beneficial effects that:|[0040] the invention provides a system for extracting a green corrosion inhibitor by supercritical carbon dioxide for carbon capture and sealing, which utilizes carbon dioxide on the carbon capture side, extracts the green corrosion inhibitor in a natural product by a supercritical extraction method, and injects the green corrosion inhibitor into a pipeline for transporting carbon dioxide. Therefore, the carbon sequestration and complement technology and the supercritical extraction method can be well coupled, and the extraction raw materials come from the carbon capture side, so that the extraction cost is reduced.|[0041] Further, the moderate crushing of the extraction by the crusher can increase the contact surface channel of the solid and the solvent, and the extraction rate is improved.|[0042] Further, a normal-temperature high-pressure liquefaction method is adopted in the process of preparing the supercritical carbon dioxide, and the method can play a role in liquefaction without low-temperature refrigeration equipment and refrigerant, so that an ozone layer is not damaged, energy sources are saved, and running cost is reduced.|[0043] Further, the green corrosion inhibitor can be extracted more effectively by strictly controlling the water content of the extraction raw material through the dryer.|[0044] Further, the pressure and temperature of the green corrosion inhibitor active ingredient when separating from the rectifying tower and the pressure and temperature when converting the carbon dioxide source to be transported from the carbon capturing side into supercritical carbon dioxide need to be far away from the critical pressure and critical temperature, and the green corrosion inhibitor active ingredient has the advantages that the green corrosion inhibitor active ingredient is easy to change drastically on one hand near the critical point; on the other hand, the large change of the supercritical fluid density near the critical point can cause the content of the contained effective corrosion inhibitor component to be reduced.|[0045] Further, the carbon dioxide transportation processing module, the extraction heat exchanger, the supercritical continuous extraction device and the rectifying tower heat source are all from a carbon capture side heat source, and the utilized heat is returned to the carbon capture side.|[0046] The invention also provides a method for extracting the green corrosion inhibitor by the supercritical carbon dioxide for capturing and sealing carbon, which simplifies the technical difficulty and the process complexity of filling and separating the corrosion inhibitor, can separate the corrosion inhibitor through simple change of temperature and pressure, and further expands the application market of the supercritical carbon dioxide extraction process.|[0047] Further, the separated green corrosion inhibitor can be recycled, and the advantage of low cost is fully proved.|DRAWINGS DESCRIPTION|[0048] FIG. 1 is a schematic diagram of a supercritical carbon dioxide extraction green corrosion inhibitor system and method in accordance with the present invention;|[0049] wherein: the 01-carbon capture side is used for a supercritical carbon dioxide extraction source; 02-a purifier; 03-a compressor; 04-condenser; 05-a liquid carbon dioxide storage tank; 06-a mixer; 07-high pressure pump; 08-extraction heat exchanger; 09-extraction back pressure valve; 10-supercritical continuous extraction device; 11-extracting residues; 12-extracting the product; 13-a rectifying tower; 14-non-green corrosion inhibitor active ingredient extract and entrainer; 15-green corrosion inhibitor active ingredient; a carbon dioxide source to be transported at the 16-carbon capturing side; 17-a transport compressor; 18-a transport condenser; 19-transporting a high pressure pump; 20-a transport heat exchanger; 21-adding a green corrosion inhibitor and then transporting supercritical carbon dioxide; 22-carbon capture side heat stream source; 23-entering the extraction heat exchanger to heat flow; 24-heat flow leaving the extraction heat exchanger; 25-entering a transport heat exchanger for heat flow; 26-leaving transport heat exchanger heat flow; 27-heat flow entering a supercritical rectifying tower; 28-entrainer storage tank; 29-an entrainer auxiliary pump; 30-screening machine; 31-storing raw materials to be extracted; 32-a slicer; 33-a dryer; 34-a pulverizer; 35-a gauge; 36-direct flow to carbon sequestration or utilization side supercritical carbon dioxide stream; 37-supercritical carbon dioxide stream with green corrosion inhibitor entrained after transport; 38-a heat exchange device; 39-separation means; 40-supercritical carbon dioxide stream without green corrosion inhibitor; 41-green corrosion inhibitor separated.|INVENTION MODE|Detailed Description|[0050] In order that those skilled in the art will better understand the present invention, a technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in which it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, shall fall within the scope of the present invention.|[0051] It should be noted that the terms "first," "second," and the like in the description and the claims of the present invention and the above figures are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate such that the embodiments of the invention described herein may be implemented in sequences other than those illustrated or otherwise described herein. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.|[0052] The invention is described in further detail below with reference to fig. 1:|[0053] a supercritical carbon dioxide extraction green corrosion inhibitor system and method comprises four modules: the device comprises a supercritical carbon dioxide extractant production module, an extraction raw material pretreatment module, a carbon dioxide transportation treatment module and a green corrosion inhibitor filling and separation module. All the modules are matched with each other, connected according to the need and work together. The specific implementation process comprises the following steps:|[0054] s01, taking a small part of carbon dioxide captured and collected from a typical carbon capturing side-a coal-fired power plant as a carbon capturing side for supercritical carbon dioxide extraction source 01, and further removing impurities and dehydrating the carbon dioxide into carbon dioxide gas for extraction after passing through a purifier 02. After entering a compressor 03 and being pressurized by 7.6Mpa to 8.1Mpa, the carbon dioxide is cooled to normal temperature by a condenser 04 to be changed into carbon dioxide liquid, and the carbon dioxide liquid is stored in a liquid carbon dioxide storage tank 05 which is mainly used for ensuring uninterrupted process.|[0055] The method adopts a normal temperature and high pressure liquefaction technology to liquefy the carbon dioxide gas, and the main purpose of the liquefaction is better mixing with a liquid entrainer, and in addition, in order to save energy, a high pressure pump is generally selected to pressurize the carbon dioxide to a supercritical state.|[0056] S02, selecting whether an entrainer is needed according to the polarity and other conditions of the effective components of the green corrosion inhibitor in the extraction raw materials. The inlet end of the mixer 06 is connected with pure liquid carbon dioxide which is discharged from the liquid carbon dioxide storage tank 05, and the other end is connected with entrainer which is extracted from the entrainer storage tank 28 through the entrainer auxiliary pump 29. The entrainer auxiliary pump is a peristaltic pump. The outlet of the mixer 06 is connected with the inlet of the high-pressure pump 07 through a pipeline, the inlet of the extraction heat exchanger 08 is connected with the outlet of the high-pressure pump 07 through a pipeline, the extractant entering the high-pressure pump 07 is boosted to 7.4 Mpa-40 Mpa according to the requirement, and the extractant in a high-pressure low-temperature state is heated to 35 ℃ to 80 ℃ through the extraction heat exchanger 08 to reach a supercritical state. An extraction back pressure valve 09 is connected to the outlet of the extraction heat exchanger 08 for regulating the pressure entering the supercritical continuous extraction apparatus 10. The carbon capture side heat flux 22 splits off a portion of the heat flux 23 entering the extraction heat exchanger and the heat flux 24 leaving the extraction heat exchanger after the heat exchange is completed is returned to the carbon capture side.|[0057] Wherein the high pressure pump is of the plunger type. The extraction heat exchanger is divided into a wall type, a heat flow source passes through a shell side, and carbon dioxide passes through a tube side. The heat flow source 22 at the carbon capturing side can be flue gas waste heat (more than or equal to 100 ℃) or circulating water waste heat (30 ℃ -50 ℃) according to actual requirements. The supercritical continuous extraction device 10 is a high-pressure extraction device for continuous feeding and discharging, and can adopt a high-pressure sealed spiral conveying feeding continuous extraction device, a jet feeding continuous extraction device, a multi-kettle continuous extraction device, a spherical feeding and discharging structure continuous extractor, a magazine chain feeding and discharging structure tubular continuous extraction device, a horizontal rotation type feeding port continuous extraction device and the like.|[0058] S03, the raw materials to be extracted contain green corrosion inhibitor active ingredients, the raw materials to be extracted which are free of deterioration and insect damage are selected by the screening machine 30 and then are placed in the raw material storage bin 31 to be stored for standby, when extraction is needed, the raw materials enter the dryer 33 for drying treatment after passing through the slicer 32, and moisture is a main factor for preventing the extraction solvent from effectively contacting with the to-be-extracted substances, mutually dissolving and forming a continuous main mass transfer system with the solvent, so that strict control is needed. Then the mixture enters a pulverizer 34 to be pulverized to 80-150 meshes, and after moderate pulverization, the contact surface channel of the solid and the solvent can be increased, so that the extraction rate is improved. The raw material powder to be extracted enters the supercritical continuous extraction device 10 after being metered by the meter 35, and the content of the raw material powder to be extracted can be metered according to the flow of supercritical carbon dioxide.|[0059] S04, the supercritical continuous extraction device 10 discharges extraction residues 11, the extraction products 12 enter the rectifying tower 13, and the positions of entering and leaving the rectifying tower 13 are determined according to the types of effective components of corrosion inhibitors and entrainers contained in different raw materials to be extracted. The temperature of the rectifying tower 13 gradually rises from bottom to top, and the lowest temperature is higher than the extraction temperature. The heat stream 27 entering the supercritical rectification column 13 also comes from the carbon capture side heat source 22.|[0060] S05, taking most of carbon dioxide captured and collected from a typical carbon capturing side-a coal-fired power plant as a carbon dioxide source 16 to be transported at the carbon capturing side, changing the carbon dioxide into liquid carbon dioxide after passing through a transport compressor 17 and a transport condenser 18, wherein the pressure is between 7.6Mpa and 8.1Mpa, and the temperature is reduced to room temperature. Further becomes a supercritical state after passing through a high-pressure conveying pump 19 and a heat conveying exchanger 20, and the pressure is 7.6-21 Mpa. The heat flow 25 entering the transport heat exchanger still comes from the carbon capture side heat flow source 22.|[0061] Wherein the type of transport compressor 17, transport condenser 18, transport high pressure pump 19 and transport heat exchanger 20 are substantially similar to those described above, but with larger specifications.|[0062] S06, filling the supercritical carbon dioxide to be transported with the green corrosion inhibitor active ingredient 15, changing into filling the green corrosion inhibitor, and then filling the supercritical carbon dioxide to be transported 21, wherein the filling process is positioned between the carbon capturing side and the carbon transporting side.|[0063] S07, after reaching the carbon transport side end, there is a direct flow to the carbon sequestration or utilization side supercritical carbon dioxide stream 36. If the green corrosion inhibitor needs to be separated, the transported supercritical carbon dioxide stream 37 with the green corrosion inhibitor enters the heat exchange device 38 and the separation device 39 in sequence to change the temperature and the pressure, and then the separation is completed. The finally separated green corrosion inhibitor 41 can be recycled, the supercritical carbon dioxide stream 40 without the green corrosion inhibitor enters a carbon sequestration or utilization side, and the separated carbon dioxide is in a gaseous state, so that the next link can conveniently enter a compressor for injection into a geological sequestration area.|[0064] The above is only for illustrating the technical idea of the present invention, and the protection scope of the present invention is not limited by this, and any modification made on the basis of the technical scheme according to the technical idea of the present invention falls within the protection scope of the claims of the present invention. (CN114887351)|TECHNICAL FIELD|[0001] The invention belongs to the technical field of carbon trapping and sealing and supercritical fluid extraction corrosion inhibitors, and particularly relates to a system and a method for supercritical carbon dioxide extraction green corrosion inhibitor for carbon trapping and sealing.|BACKGROUND ART|[0002] Since the industrial revolution, the content of carbon dioxide in the atmosphere is remarkably improved, which directly causes the continuous rise of global surface temperature, the occurrence of disaster phenomena such as polar ice melting, sea level rising and the like, and serious damage is caused to the sustainable development of ecological environment and world economy. Carbon capture and sequestration technology (CCS) can separate and collect carbon dioxide from emission sources in a closed loop and transport a large amount to relevant areas for sequestration, and is a main means for slowing down climate change, and mainly consists of three links of capture, transportation and sequestration. The pipeline transportation technology is suitable for long-distance and large-output requirements. Carbon dioxide is generally transported in supercritical state from the viewpoints of economy and avoiding two-phase flow. Although certain requirements are imposed on the quality of the captured carbon dioxide gas, such as the water content, the hydrogen sulfide content, etc., in terms of design and health safety, etc., strict control is required, it is impossible to obtain completely pure carbon dioxide from the practical operation and economical point of view. However, the presence of these impurities can cause corrosion problems inside the pipe. The occurrence of corrosion in the supercritical carbon dioxide pipeline not only causes huge economic loss, but also brings about great potential safety hazard. The addition of a certain amount of corrosion inhibitor to the conveying pipeline is the most economical and effective corrosion control means at present, but part of the corrosion inhibitor such as chromate, mercury salt and the like is toxic, and other main flow corrosion inhibitors have different degrees and can have certain influence on the environment. The captured carbon dioxide will eventually be transported deep underground into long-term or permanently buried bodies such as oil and gas fields, salt water aquifers deposited in basins, coal seams, deep sea, and the like. It is rather a counter-operation if the harmful corrosion inhibitors are discharged into the geological environment in order to slow down the carbon dioxide pollution. Meanwhile, the corrosion inhibitor carried in the supercritical carbon dioxide pipeline is subjected to cleaning treatment at the conveying end, and the technical difficulty and the economic cost are huge.|[0003] The use of the natural green corrosion inhibitor can improve the conditions, and the natural green corrosion inhibitor has the characteristics of low toxicity and no pollution, and can reduce the harm of organic corrosion inhibitors and the like to human bodies and the environment in industrial production. Related studies have extracted effective components having corrosion inhibition effects from natural plants, marine plants and plant wastes for inhibiting pipeline corrosion. The plant corrosion inhibitor can be extracted from leaves, fruits, roots, seeds, etc. of plants. Early domestic related researchers extract corrosion inhibition effective components from reed and water lily leaves and stems and obtain good results, and then extract corrosion inhibition effective components in plants such as tea, pepper, pericarp, phellodendron and the like, so that corrosion inhibition effects with different degrees are obtained.|[0004] The extraction method of the plant corrosion inhibitor is various, and common extraction methods include a soaking method, a heating reflux method, a Soxhlet extraction method, an enzymolysis method, an ultrasonic extraction method, a microwave extraction method and the like. The soaking method is simple and convenient to operate, but has the problems of low efficiency, low extraction rate and the like; the heating reflux method and the Soxhlet extraction method have similar extraction principles and long extraction time, but the Soxhlet extraction method has the advantages of less solvent and high extraction efficiency; in addition, the Soxhlet extraction method has high extraction temperature, and the problem of temperature resistance of the plant extract should be considered; the enzyme activity in the enzymolysis method is related to temperature, pH, reactant concentration and the like, has extremely severe requirements on the extraction environment and has a narrow application range; the ultrasonic extraction method has high extraction efficiency, but the electric energy consumption is a main limiting factor.|[0005] Supercritical Fluid Extraction (SFE) is a new green separation technique and has been rapidly developed. The supercritical carbon dioxide extraction adopts carbon dioxide as a solvent, and carbon dioxide is used as a supercritical fluid, the critical temperature is 31.1 ℃, the critical pressure is 7.39MPa, the operation temperature and the operation pressure are easy to realize, and the energy consumption is low. The supercritical carbon dioxide fluid has high density and dielectric constant, has strong dissolving power to many substances, has a separation rate far faster than that of liquid extraction, and changes sharply along with the change of pressure and temperature, so that the supercritical carbon dioxide fluid has selectivity to the solubility of certain substances, and the solvent and the extract are easy to separate. Compared with the conventional separation method, the supercritical carbon dioxide extraction technology does not use an organic solvent and has no solvent residue; heavy metal and pesticide residues are avoided; no waste gas, waste water and waste residue exists in the whole process; has the advantages of low extraction temperature, strong selectivity, high efficiency, low energy consumption, no pollution and the like. Supercritical carbon dioxide extraction is currently mainly focused on plant essential oil, natural pigment, alkaloid (one of the effective components of traditional Chinese medicine) and the like.|[0006] Therefore, in order to solve the problems of internal corrosion in a supercritical carbon dioxide transportation pipeline, environmental hazard caused by the use of partial corrosion inhibitors, insufficient extraction methods of traditional plant corrosion inhibitors and the like, a green, environment-friendly, energy-saving and economic process method is needed.|DISCLOSURE|Disclosure of Invention|[0007] In order to overcome the defects and imperfections of the prior art, the invention aims to provide a system and a method for extracting a green corrosion inhibitor by supercritical carbon dioxide for carbon capture and sealing, which can solve the problems of corrosion in a supercritical carbon dioxide transportation pipeline and difficult extraction of a plant corrosion inhibitor, save energy consumption and reduce economic cost.|[0008] In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:|[0009] the invention provides a system for supercritical carbon dioxide extraction green corrosion inhibitor for carbon capture and sequestration, which is characterized by comprising an extraction raw material pretreatment module, a supercritical carbon dioxide extractant production module, a carbon dioxide transportation treatment module, a green corrosion inhibitor filling and separating module and a carbon transportation side, wherein the extraction raw material pretreatment module, the supercritical carbon dioxide extractant production module, the carbon dioxide transportation treatment module, the green corrosion inhibitor filling and separating module and the carbon transportation side are arranged between a carbon capture side and a carbon sequestration or utilization side.|[0010] The extraction raw material pretreatment module comprises a screening machine, a raw material storage bin to be extracted, a slicing machine, a dryer, a pulverizer and a meter.|[0011] The supercritical carbon dioxide extractant production module comprises a liquid carbon dioxide pretreatment unit, an extraction heat exchanger, an extraction backpressure valve and a supercritical continuous extraction device which are connected in sequence.|[0012] The liquid carbon dioxide pretreatment unit comprises a purifier, a compressor, a condenser and a liquid carbon dioxide storage tank which are sequentially connected, wherein the outlet end of the liquid carbon dioxide storage tank is connected with the inlet of one end of a mixer, the inlet of the other end of the mixer is connected with an entrainer auxiliary pump, the entrainer auxiliary pump is connected with the entrainer storage tank, the outlet end of the mixer is connected with the inlet end of a high-pressure pump, and the outlet end of the high-pressure pump is connected with an extraction heat exchanger.|[0013] And the inlet end at one side of the supercritical continuous extraction device is connected with the outlet end of the metering device of the extraction raw material pretreatment module, and the outlet end is connected with the rectifying tower of the green corrosion inhibitor filling and separating module.|[0014] The carbon dioxide conveying treatment module comprises a conveying compressor, a conveying condenser, a conveying high-pressure pump and a conveying heat exchanger which are sequentially connected, wherein the inlet end of the conveying compressor is connected with the carbon complement side through a pipeline, and the outlet end of the conveying heat exchanger is connected with the green corrosion inhibitor filling and separating module through a pipeline.|[0015] The green corrosion inhibitor filling and separating module comprises a rectifying tower and a green corrosion inhibitor separating unit, wherein the outlet end of the rectifying tower is introduced into the tail end of an outlet pipeline of the conveying heat exchanger, the tail end of the outlet pipeline of the conveying heat exchanger is connected to a carbon conveying side, and the outlet of the carbon conveying side is connected with the green corrosion inhibitor separating unit.|[0016] The green corrosion inhibitor separation unit comprises a heat exchange device and a separation device which are connected, wherein an outlet at one end of a carbon transportation side is directly connected with a carbon sealing or utilizing side, the other end of the carbon transportation side is connected with an inlet end of the heat exchange device, an outlet end of the heat exchange device is connected with the separation device, and an outlet of the separation device is connected with the carbon sealing or utilizing side.|[0017] Preferably, the entrainer auxiliary pump is a peristaltic pump; the supercritical continuous extraction device is a high-pressure extraction device for continuously feeding and discharging materials; the high-pressure pump and the high-pressure conveying pump are of plunger pump type, and particularly, a pump head sealing structure and a sealing material are required to be suitable for supercritical carbon dioxide fluid, and the sealing material such as graphite and oil-resistant rubber can face failure risks due to extremely strong extraction of the supercritical carbon dioxide fluid; the extraction heat exchanger and the transportation heat exchanger are of partition wall type, heat flow entering the extraction heat exchanger and the transportation heat exchanger passes through a shell side, and carbon dioxide passes through a tube side.|[0018] Preferably, the carbon capture side heat source is flue gas waste heat (more than or equal to 100 ℃) or circulating water waste heat (30-50 ℃).|[0019] Further preferably, the extraction heat exchanger, the transportation heat exchanger and the rectifying tower are all provided with pipelines for acquiring heat sources at the carbon capturing side, and the extraction heat exchanger and the transportation heat exchanger are provided with pipelines for returning waste heat to the carbon capturing side.|[0020] Further preferably, the purifier removes impurity gases, absorbents and moisture to meet the carbon dioxide standard for supercritical fluid extraction.|[0021] Further preferably, the size of the raw material powder to be extracted is 80-150 meshes.|[0022] Further preferably, the meter measures the raw material powder content to be extracted according to the supercritical carbon dioxide flow rate.|[0023] Supercritical carbon dioxide extraction has certain requirements on flow, and if the flow of carbon dioxide is increased, the mass transfer effect in the extraction process can be enhanced, and the solute which is rapidly dissolved is carried out from the raw material, so that the extraction time is shortened. Typically, the ratio of extract to carbon dioxide is about 1:20. The flow rate of the carbon dioxide is too fast, the residence time in the extraction kettle is shortened, the contact time with the extracted matter is shortened, and the solute content in the carbon dioxide is reduced. The flow rate of carbon dioxide is too slow, the residence time in the extraction kettle is prolonged, the contact time with the extracted substance is increased, the solute content in the carbon dioxide is increased, and the extraction time is prolonged.|[0024] Further preferably, the dryer requires strict control of the extraction feed moisture.|[0025] Further preferably, the pressure of the compressor is raised to 7.6Mpa to 8.1Mpa, and the temperature of the condenser is lowered to room temperature.|[0026] Further preferably, the pressure of the high-pressure pump is raised to 7.4Mpa to 40Mpa, and the temperature of the extraction heat exchanger is raised to 35 ℃ to 80 ℃.|[0027] Further preferably, the rectifying column temperature is higher than the extraction temperature of the supercritical continuous extraction device.|[0028] Further preferably, the pressure of the conveying compressor is increased to 7.6-8.1 Mpa, the conveying condenser is cooled to room temperature, and the pressure of the conveying high-pressure pump is increased to 7.6-21 Mpa.|[0029] The supercritical fluid extraction and supercritical carbon dioxide pipeline transportation are all gaseous carbon dioxide. There are two general schemes for converting gaseous carbon dioxide into supercritical carbon dioxide, one is to directly convert the gaseous carbon dioxide into supercritical carbon dioxide by a compressor, but a large volume of compressor is required for preparing the supercritical carbon dioxide, and a large temperature rise is generated in the isenthalpic compression process; and secondly, liquefying the carbon dioxide, and then obtaining the supercritical carbon dioxide by using a high-pressure pump. The invention adopts a second liquefaction scheme:|[0030] the invention adopts the scheme of liquefying at normal temperature and high pressure, even if gaseous carbon dioxide is converted into liquid state at normal temperature. When the temperature is 31.16 ℃ and the pressure is 7.6Mpa, the carbon dioxide starts to liquefy, and when the temperature in summer is high, the final pressure of the compressor can reach 8.1Mpa.|[0031] Preferably, the pressure and temperature of the green corrosion inhibitor active ingredient when separated from the rectifying tower are matched with the pressure and temperature when the carbon dioxide source to be transported from the carbon capturing side is converted into supercritical carbon dioxide, and the pressure and the temperature are far away from the critical pressure and the critical temperature. The values of the far-away range should be comprehensively considered, and the aspects of economy, safety and the like should be included, so that the far-away range is not suitable.|[0032] The invention also provides a method for extracting the green corrosion inhibitor by supercritical carbon dioxide, which comprises the following steps:|[0033] s01, carbon dioxide generated by the carbon complement side is processed by the liquid carbon dioxide pretreatment unit to be changed into liquid carbon dioxide, and then enters an extraction heat exchanger to be converted into supercritical carbon dioxide;|[0034] s02, the supercritical carbon dioxide enters a supercritical continuous extraction device after the pressure is regulated by an extraction back pressure valve, and is extracted with the natural product processed by the extraction raw material pretreatment module to generate an extraction product;|[0035] s03, carbon dioxide generated by the carbon capturing side is processed by a carbon dioxide transportation processing module to be changed into supercritical carbon dioxide, and then the supercritical carbon dioxide is connected to the carbon transportation side;|[0036] s04, the extracted product enters a rectifying tower to separate out the effective components of the green corrosion inhibitor, and the effective components are connected into the supercritical carbon dioxide of the S03, and carbon sealing and utilization are completed.|[0037] Preferably, the extracted natural product contains green corrosion inhibitor active ingredients.|[0038] Preferably, the carbon capture to-be-transported carbon dioxide source is from a typical carbon capture side, namely a large amount of carbon dioxide captured and collected by a coal-fired power plant, and the impurity content is required to meet the standard of a transportation pipeline.|[0039] Compared with the prior art, the invention has the beneficial effects that:|[0040] the invention provides a system for extracting a green corrosion inhibitor by supercritical carbon dioxide for carbon capture and sealing, which utilizes carbon dioxide on the carbon capture side, extracts the green corrosion inhibitor in a natural product by a supercritical extraction method, and injects the green corrosion inhibitor into a pipeline for transporting carbon dioxide. Therefore, the carbon sequestration and complement technology and the supercritical extraction method can be well coupled, and the extraction raw materials come from the carbon capture side, so that the extraction cost is reduced.|[0041] Further, the moderate crushing of the extraction by the crusher can increase the contact surface channel of the solid and the solvent, and the extraction rate is improved.|[0042] Further, a normal-temperature high-pressure liquefaction method is adopted in the process of preparing the supercritical carbon dioxide, and the method can play a role in liquefaction without low-temperature refrigeration equipment and refrigerant, so that an ozone layer is not damaged, energy sources are saved, and running cost is reduced.|[0043] Further, the green corrosion inhibitor can be extracted more effectively by strictly controlling the water content of the extraction raw material through the dryer.|[0044] Further, the pressure and temperature of the green corrosion inhibitor active ingredient when separating from the rectifying tower and the pressure and temperature when converting the carbon dioxide source to be transported from the carbon capturing side into supercritical carbon dioxide need to be far away from the critical pressure and critical temperature, and the green corrosion inhibitor active ingredient has the advantages that the green corrosion inhibitor active ingredient is easy to change drastically on one hand near the critical point; on the other hand, the large change of the supercritical fluid density near the critical point can cause the content of the contained effective corrosion inhibitor component to be reduced.|[0045] Further, the carbon dioxide transportation processing module, the extraction heat exchanger, the supercritical continuous extraction device and the rectifying tower heat source are all from a carbon capture side heat source, and the utilized heat is returned to the carbon capture side.|[0046] The invention also provides a method for extracting the green corrosion inhibitor by the supercritical carbon dioxide for capturing and sealing carbon, which simplifies the technical difficulty and the process complexity of filling and separating the corrosion inhibitor, can separate the corrosion inhibitor through simple change of temperature and pressure, and further expands the application market of the supercritical carbon dioxide extraction process.|[0047] Further, the separated green corrosion inhibitor can be recycled, and the advantage of low cost is fully proved.|DRAWINGS DESCRIPTION|[0048] FIG. 1 is a schematic diagram of a supercritical carbon dioxide extraction green corrosion inhibitor system and method in accordance with the present invention;|[0049] wherein: the 01-carbon capture side is used for a supercritical carbon dioxide extraction source; 02-a purifier; 03-a compressor; 04-condenser; 05-a liquid carbon dioxide storage tank; 06-a mixer; 07-high pressure pump; 08-extraction heat exchanger; 09-extraction back pressure valve; 10-supercritical continuous extraction device; 11-extracting residues; 12-extracting the product; 13-a rectifying tower; 14-non-green corrosion inhibitor active ingredient extract and entrainer; 15-green corrosion inhibitor active ingredient; a carbon dioxide source to be transported at the 16-carbon capturing side; 17-a transport compressor; 18-a transport condenser; 19-transporting a high pressure pump; 20-a transport heat exchanger; 21-adding a green corrosion inhibitor and then transporting supercritical carbon dioxide; 22-carbon capture side heat stream source; 23-entering the extraction heat exchanger to heat flow; 24-heat flow leaving the extraction heat exchanger; 25-entering a transport heat exchanger for heat flow; 26-leaving transport heat exchanger heat flow; 27-heat flow entering a supercritical rectifying tower; 28-entrainer storage tank; 29-an entrainer auxiliary pump; 30-screening machine; 31-storing raw materials to be extracted; 32-a slicer; 33-a dryer; 34-a pulverizer; 35-a gauge; 36-direct flow to carbon sequestration or utilization side supercritical carbon dioxide stream; 37-supercritical carbon dioxide stream with green corrosion inhibitor entrained after transport; 38-a heat exchange device; 39-separation means; 40-supercritical carbon dioxide stream without green corrosion inhibitor; 41-green corrosion inhibitor separated.|INVENTION MODE|Detailed Description|[0050] In order that those skilled in the art will better understand the present invention, a technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in which it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, shall fall within the scope of the present invention.|[0051] It should be noted that the terms "first," "second," and the like in the description and the claims of the present invention and the above figures are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate such that the embodiments of the invention described herein may be implemented in sequences other than those illustrated or otherwise described herein. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.|[0052] The invention is described in further detail below with reference to fig. 1:|[0053] a supercritical carbon dioxide extraction green corrosion inhibitor system and method comprises four modules: the device comprises a supercritical carbon dioxide extractant production module, an extraction raw material pretreatment module, a carbon dioxide transportation treatment module and a green corrosion inhibitor filling and separation module. All the modules are matched with each other, connected according to the need and work together. The specific implementation process comprises the following steps:|[0054] s01, taking a small part of carbon dioxide captured and collected from a typical carbon capturing side-a coal-fired power plant as a carbon capturing side for supercritical carbon dioxide extraction source 01, and further removing impurities and dehydrating the carbon dioxide into carbon dioxide gas for extraction after passing through a purifier 02. After entering a compressor 03 and being pressurized by 7.6Mpa to 8.1Mpa, the carbon dioxide is cooled to normal temperature by a condenser 04 to be changed into carbon dioxide liquid, and the carbon dioxide liquid is stored in a liquid carbon dioxide storage tank 05 which is mainly used for ensuring uninterrupted process.|[0055] The method adopts a normal temperature and high pressure liquefaction technology to liquefy the carbon dioxide gas, and the main purpose of the liquefaction is better mixing with a liquid entrainer, and in addition, in order to save energy, a high pressure pump is generally selected to pressurize the carbon dioxide to a supercritical state.|[0056] S02, selecting whether an entrainer is needed according to the polarity and other conditions of the effective components of the green corrosion inhibitor in the extraction raw materials. The inlet end of the mixer 06 is connected with pure liquid carbon dioxide which is discharged from the liquid carbon dioxide storage tank 05, and the other end is connected with entrainer which is extracted from the entrainer storage tank 28 through the entrainer auxiliary pump 29. The entrainer auxiliary pump is a peristaltic pump. The outlet of the mixer 06 is connected with the inlet of the high-pressure pump 07 through a pipeline, the inlet of the extraction heat exchanger 08 is connected with the outlet of the high-pressure pump 07 through a pipeline, the extractant entering the high-pressure pump 07 is boosted to 7.4 Mpa-40 Mpa according to the requirement, and the extractant in a high-pressure low-temperature state is heated to 35 ℃ to 80 ℃ through the extraction heat exchanger 08 to reach a supercritical state. An extraction back pressure valve 09 is connected to the outlet of the extraction heat exchanger 08 for regulating the pressure entering the supercritical continuous extraction apparatus 10. The carbon capture side heat flux 22 splits off a portion of the heat flux 23 entering the extraction heat exchanger and the heat flux 24 leaving the extraction heat exchanger after the heat exchange is completed is returned to the carbon capture side.|[0057] Wherein the high pressure pump is of the plunger type. The extraction heat exchanger is divided into a wall type, a heat flow source passes through a shell side, and carbon dioxide passes through a tube side. The heat flow source 22 at the carbon capturing side can be flue gas waste heat (more than or equal to 100 ℃) or circulating water waste heat (30 ℃ -50 ℃) according to actual requirements. The supercritical continuous extraction device 10 is a high-pressure extraction device for continuous feeding and discharging, and can adopt a high-pressure sealed spiral conveying feeding continuous extraction device, a jet feeding continuous extraction device, a multi-kettle continuous extraction device, a spherical feeding and discharging structure continuous extractor, a magazine chain feeding and discharging structure tubular continuous extraction device, a horizontal rotation type feeding port continuous extraction device and the like.|[0058] S03, the raw materials to be extracted contain green corrosion inhibitor active ingredients, the raw materials to be extracted which are free of deterioration and insect damage are selected by the screening machine 30 and then are placed in the raw material storage bin 31 to be stored for standby, when extraction is needed, the raw materials enter the dryer 33 for drying treatment after passing through the slicer 32, and moisture is a main factor for preventing the extraction solvent from effectively contacting with the to-be-extracted substances, mutually dissolving and forming a continuous main mass transfer system with the solvent, so that strict control is needed. Then the mixture enters a pulverizer 34 to be pulverized to 80-150 meshes, and after moderate pulverization, the contact surface channel of the solid and the solvent can be increased, so that the extraction rate is improved. The raw material powder to be extracted enters the supercritical continuous extraction device 10 after being metered by the meter 35, and the content of the raw material powder to be extracted can be metered according to the flow of supercritical carbon dioxide.|[0059] S04, the supercritical continuous extraction device 10 discharges extraction residues 11, the extraction products 12 enter the rectifying tower 13, and the positions of entering and leaving the rectifying tower 13 are determined according to the types of effective components of corrosion inhibitors and entrainers contained in different raw materials to be extracted. The temperature of the rectifying tower 13 gradually rises from bottom to top, and the lowest temperature is higher than the extraction temperature. The heat stream 27 entering the supercritical rectification column 13 also comes from the carbon capture side heat source 22.|[0060] S05, taking most of carbon dioxide captured and collected from a typical carbon capturing side-a coal-fired power plant as a carbon dioxide source 16 to be transported at the carbon capturing side, changing the carbon dioxide into liquid carbon dioxide after passing through a transport compressor 17 and a transport condenser 18, wherein the pressure is between 7.6Mpa and 8.1Mpa, and the temperature is reduced to room temperature. Further becomes a supercritical state after passing through a high-pressure conveying pump 19 and a heat conveying exchanger 20, and the pressure is 7.6-21 Mpa. The heat flow 25 entering the transport heat exchanger still comes from the carbon capture side heat flow source 22.|[0061] Wherein the type of transport compressor 17, transport condenser 18, transport high pressure pump 19 and transport heat exchanger 20 are substantially similar to those described above, but with larger specifications.|[0062] S06, filling the supercritical carbon dioxide to be transported with the green corrosion inhibitor active ingredient 15, changing into filling the green corrosion inhibitor, and then filling the supercritical carbon dioxide to be transported 21, wherein the filling process is positioned between the carbon capturing side and the carbon transporting side.|[0063] S07, after reaching the carbon transport side end, there is a direct flow to the carbon sequestration or utilization side supercritical carbon dioxide stream 36. If the green corrosion inhibitor needs to be separated, the transported supercritical carbon dioxide stream 37 with the green corrosion inhibitor enters the heat exchange device 38 and the separation device 39 in sequence to change the temperature and the pressure, and then the separation is completed. The finally separated green corrosion inhibitor 41 can be recycled, the supercritical carbon dioxide stream 40 without the green corrosion inhibitor enters a carbon sequestration or utilization side, and the separated carbon dioxide is in a gaseous state, so that the next link can conveniently enter a compressor for injection into a geological sequestration area.|[0064] The above is only for illustrating the technical idea of the present invention, and the protection scope of the present invention is not limited by this, and any modification made on the basis of the technical scheme according to the technical idea of the present invention falls within the protection scope of the claims of the present invention. Family Number|(101303669)|101303669|Abstract|(CN114887351B B)|The invention discloses a supercritical carbon dioxide extraction green corrosion inhibitor system and method , and belongs to the technical field of carbon capture and storage and supercritical fluid extraction , and the method comprises the following steps : extracting part of carbon dioxide from a carbon capture side , purifying , liquefying , uniformly mixing with an entrainer , feeding into a high - pressure pump and a heat exchanger , converting into a supercritical extraction agent , an extraction raw material enters a continuous extraction device after being subjected to fine screening , slicing , drying and crushing , an entrainer is separated after the green corrosion inhibitor obtained through extraction passes through a rectifying tower , the entrainer is injected into a carbon capture side to - be - transported supercritical carbon dioxide , whether effective components of the corrosion inhibitor are separated or not is selected according to requirements , and carbon dioxide can be completely separated and obtained only by changing pressure and temperature during separation . The whole technological process is green and environment - friendly , energy is saved , the application scene of supercritical fluid extraction is further expanded , and the development of the carbon capture and storage technology is also promoted . |CPC codes|(CN114887351B B)|B01D - 011/02/03 |B01D - 011/02/88 |IPC codes|(CN114887351B B)|B01D - 011/02 |Title|(CN114887351B B)|System and method for supercritical carbon dioxide extraction of green corrosion inhibitor for carbon capture and sequestration | Chemical engineering B01D-011/02/03|B01D-011/02/88|Y02P-020/54 B01D-011/02/03|B01D-011/02/88|Y02P-020/54 B01D-011/02 B01D-011/02 CN115044909|CN113457203|CN110499511|CN113773685|US20210039013|CN112957765 CN115044909 101747630 WHO=Examiner SELF=N CAT=Y|CN113457203 96332905 WHO=Examiner SELF=N CAT=Y|CN110499511 86760797 WHO=Examiner SELF=N CAT=Y|CN113773685 97600764 WHO=Examiner SELF=N CAT=A|US20210039013 92673035 WHO=Examiner SELF=N CAT=A|CN112957765 94733862 WHO=Examiner SELF=N CN110499511; US20210039013; CN113457203; CN113773685; CN115044909; CN112957765 GRANTED (CN114887351)|GRANTED ALIVE (CN114887351)|ALIVE (CN114887351)|LEGAL DETAILS FOR CN114887351|Actual or expected expiration date=2042-05-31|Legal state=ALIVE|Status=GRANTED|Event publication date=2022-05-31|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202210611205|Application date=2022-05-31|Standardized application number=2022CN-0611205|Event publication date=2022-08-12|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN114887351|Publication stage code=A|Publication date=2022-08-12|Standardized publication number=CN114887351|Event publication date=2022-08-12|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2022-08-30|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination|Event publication date=2023-04-28|Event code=CN/B|Event indicator=Pos|Event group=Event indicating In Force|Granted patent for invention|Publication country=CN|Publication number=CN114887351|Publication stage code=B|Publication date=2023-04-28|Standardized publication number=CN114887351B|Event publication date=2023-04-28|Event code=CN/GR01|Event indicator=Pos|Event group=Event indicating In Force|Grant of patent right (CN114887351)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQpt/JChSeyHxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067617245&ekey=2089&xpn=CN114887351B&kind=B https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=GrXOt%252BuaH7wyOTUsfMrTrbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT CN (CN114887351)|CN|(CN114887351)|CN (CN114887351)|NAME=XI'AN JIAOTONG UNIVERSITY , COUNTRY=CN|(CN114887351)|NAME=XI'AN JIAOTONG UNIVERSITY , COUNTRY=CN (CN114887351)|NAME=FAN WEI;XI'AN TONG DA (TONG SHENG) PATENT & TRADEMARK AGENCY CO. LTD. , REG=61200|(CN114887351)|NAME=FAN WEI;XI'AN TONG DA (TONG SHENG) PATENT & TRADEMARK AGENCY CO. LTD. , REG=61200 (CN114887351)|NAME=Wang Yueshe|NAME=Tong Guohu|NAME=Wang Xiaodan|NAME=Li Ruidong|(CN114887351)|NAME=WANG YUESHE|NAME=TONG GUOHU|NAME=WANG XIAODAN|NAME=LI RUIDONG 0 1 Titre: (CN114887351)|System and method for supercritical carbon dioxide extraction of green corrosion inhibitor for carbon capture and sequestration Résumé: (CN114887351)|The invention discloses a supercritical carbon dioxide extraction green corrosion inhibitor system and method, and belongs to the technical field of carbon capture and storage and supercritical fluid extraction, and the method comprises the following steps: extracting part of carbon dioxide from a carbon capture side, purifying, liquefying, uniformly mixing with an entrainer, feeding into a high-pressure pump and a heat exchanger, converting into a supercritical extraction agent, an extraction raw material enters a continuous extraction device after being subjected to fine screening, slicing, drying and crushing, an entrainer is separated after the green corrosion inhibitor obtained through extraction passes through a rectifying tower, the entrainer is injected into a carbon capture side to-be-transported supercritical carbon dioxide, whether effective components of the corrosion inhibitor are separated or not is selected according to requirements, and carbon dioxide can be completely separated and obtained only by changing pressure and temperature during separation. The whole technological process is green and environment-friendly, energy is saved, the application scene of supercritical fluid extraction is further expanded, and the development of the carbon capture and storage technology is also promoted. 125 Abstract gpt-4o-mini no The article focuses on supercritical carbon dioxide extraction for a corrosion inhibitor, which is related to carbon capture but does not involve accelerated weathering or mineral carbonation processes.
126 JP2014043557|WOJP2015/050310 WOJP2015/050310|IN201647033400|MYPI2016702815|JP2016506155|IDP00201605910|TH20161005111|KR10-2016-7021574|CN201580009148 MY183200|IN334931|JP6476165|ID2017/10506|TH166474|IN201647033400|KR10-2016-0129842|CN106029599|JPWO2015/133161|WO2015/133161 70851444 WO2015/133161 A1 2015-09-11 [WO2015133161]|IN334931 B 2020-03-17 [IN-334931]|IN201647033400 A 2016-12-02 [IN201647033400]|MY183200 A 2021-02-18 [MY-183200]|JP6476165 B2 2019-03-06 [JP6476165]|JPWO2015/133161 A1 2015-09-11 [JP2015133161W]|ID2017/10506 A 2017-09-29 [ID201710506]|TH166474 A 2017-08-24 [TH-166474]|KR10-2016-0129842 A 2016-11-09 [KR20160129842]|CN106029599 A 2016-10-12 [CN106029599] 2014-03-06|2015-01-08 2015-01-08|2016-09-30|2015-01-08|2015-01-08|2015-01-08|2015-01-08|2015-01-08|2015-01-08 2021-02-18|2020-03-17|2019-03-06|2017-09-29|2017-08-24|2016-12-02|2016-11-09|2016-10-12|2015-09-11|2015-09-11 |(JP6476165)|2019-03-06||(MY-183200)|2021-02-18|(IN-334931)|2020-03-17||| (WO2015/133161)|2017-09-06|(JP6476165)|2023-02-08|(CN106029599)|2021-11-05|(MY183200)|2035-01-08|(IN334931)|2035-01-08|(ID2017/10506)|2022-09-29|(TH166474)|2022-08-24|(KR10-2016-0129842)|2021-10-25 (WO2015/133161)|Cement burning apparatus, and method for denitrating exhaust gas from cement kiln (WO2015/133161)|[Problem] To efficiently reduce the concentration of NOx in an exhaust gas from a cement kiln while keeping the burned state at a good level regardless of the type of a calcining furnace to be used. [Solution] A cement burning apparatus (1) equipped with a burner (14) for blowing a fuel (F3) and combustion air into a kiln tail part (4) of a cement kiln (5) to burn the fuel. It becomes possible to reduce NOx, which is contained in an exhaust gas from the cement kiln, in a low-oxygen zone in the kiln tail part, and it also becomes possible to improve the decarbocxylation efficiency of a cement raw material due to the burning of the fuel. The burner may be equipped with a swirl vane (a swirl means) (14b) for swirling a mixed flow of the fuel and the combustion air. It is preferred that the amount of the fuel to be supplied into the kiln tail part of the cement kiln is 20% or more and less than 50% of the amount of the fuel to be supplied into a calcining furnace (3) that is provided in the cement kiln. The fuel to be supplied into the kiln tail part of the cement kiln may comprise at least one of pulverized coal, a heavy oil and a burnable waste material. TAIHEIYO CEMENT|TAIHEIYO ENGINEERING (WO2015/133161)|TAIHEIYO ENGINEERING CORPORATION ([JP])|(JP6476165)|TAIHEIYO ENGINEERING CORPORATION|(JPWO2015/133161)|TAIHEIYO ENGINEERING CORPORATION|(CN106029599)|TAIHEIYO CEMENT CORP. ([JP])|(MY183200)|TAIHEIYO ENGINEERING CORPORATION|(IN334931)|TAIHEIYO ENGINEERING CORPORATION|(IN201647033400)|TAIHEIYO ENGINEERING CORPORATION|(ID2017/10506)|TAIHEIYO ENGINEERING CORPORATION ([JP])|(TH166474)|Taihei Engineering Corporation|(KR10-2016-0129842)|TAIHEIYO ENGINEERING CORPORATION SUZUKI HIDETO (WO2015/133161)|SUZUKI Hideto (WO2015/133161)|NAKAI Jun ([JP])|(JP6476165)|NAKAI, Jun|Reg. Nb: 100106563|(CN106029599)|WANG YONGHONG;CCPIT PATENT & TRADEMARK LAW OFFICE|Reg. Nb: 11038|(ID2017/10506)|Dora Am Badar S Psi|(TH166474)|Mr. Chakrapit Mongkolsit, Miss Jaiyot Srikitjaaporn, Mr. Ruth Nopkhun|(KR10-2016-0129842)|Y.S.CHANG & ASSOCIATES|Reg. Nb: 920171002811 (WO2015/133161)|Furthermore, in the method described in Patent Document 2, the form of the calcination furnace is limited, and thus, a calcination furnace of a different form from the calcination furnace described in the same document does not achieve a NOx removal effect. Therefore, the present invention was conceived in view of the problems of the conventional technology described above, and an object of the present invention is to efficiently reduce the NOx concentration in the exhaust gas of the cement kiln while maintaining a favorable fired state regardless of the type of calcination furnace.|However, in a method using urea as a NOx removal agent, urea is expensive, and thus operation costs rise.| (WO2015/133161)|1. A cement calcination device provided with a burner for combusting fuel by blowing fuel and combustion air into a kiln tail of a cement kiln.|3. A method for NOx removal of cement kiln exhaust gas, comprising blowing fuel and combustion air into a kiln tail of a cement kiln to combust the fuel.| (WO2015/133161)|In addition, the present invention is a method for NOx removal of cement kiln exhaust gas, the method comprising blowing fuel and combustion air into the kiln tail of the cement kiln to combust the fuel.|The present invention relates to a technique for reducing nitrogen oxide (hereinafter referred to as "NOx") concentration in a combustion gas discharged from a cement kiln.| (WO2015/133161)|CEMENT KILN(100,45)|EXHAUST GAS(100,20)|CEMENT KILN EXHAUST GAS(100,16)|NOX REMOVAL(100,15)|COMBUSTION AIR(100,12)|BURNER(100,11)|KILN TAIL(100,9)|CEMENT(100,8)|FUEL COMBUSTION(100,6)|CEMENT CALCINATION(100,5)|BLOWING FUEL(100,4)|CEMENT KILN TAIL(100,2)|DENITRATING EXHAUST GAS(100,1)|CALCINING FURNACE(75,20)|NOX(23,16)|SWIRL VANE(23,4)|KILN(19,12)|NOX REMOVAL BURNER(18,13)|COMBUSTIBLE WASTE(18,4)|PULVERIZED COAL(16,6)|CEMENT RAW MATERIAL DECARBOCXYLATION(15,1)|UREA(14,5)|CALCINING FURNACE BURNER(14,3)|CLINKER COOLER(13,5)|REDUCING NITROGEN OXIDE(11,1)|CEMENT CALCINATION NOX(10,1)|MIXED FLOW(9,3)|BURNABLE WASTE MATERIAL(9,1)|NITROGEN OXIDE(9,1)|HEAVY OIL(7,5)|CEMENT DECARBOXYLATION(7,1)|COMBUSTION GAS(6,3)|POLYAMIDE RESIN(6,2)|LOW OXYGEN ZONE(6,1)|NONCATALYZED NOX REMOVAL(6,1)|STAGE CYCLONE(5,2)|LOWERMOST CYCLONE OUTLET GAS(5,1)|SWIRLER BLADE(5,1)|OXYGEN REGION(4,3)|UREA RESIN(4,2)|FIRE ZONE(4,1)|CYLINDRICAL MEMBER(3,5)|CEMENT CLINKER(3,2)|CEMENT RAW MATERIAL DECARBOXYLATION(3,2)|MEDIAN(3,2)|SWIRL ANGLE(3,2)|CHIMNEY EXHAUST GAS(3,1)|EXCESS AMMONIA(3,1)||(JP6476165)|CEMENT KILN(100,37)|FUEL(100,26)|CALCINING FURNACE(100,18)|EXHAUST GAS(100,18)|KILN(100,17)|CEMENT KILN EXHAUST GAS(100,16)|NOX REMOVAL BURNER(100,16)|NOX REMOVAL(100,15)|COMBUSTION AIR(100,10)|BURNER(100,8)|CEMENT(100,7)|FUEL COMBUSTION(100,5)|KILN TAIL(100,4)|BLOWING FUEL(100,3)|NOX(29,14)|COMBUSTIBLE WASTE(29,4)|CARBONYLDIAMIDE(26,5)|CALCINING FURNACE BURNER(22,3)|CLINKER COOLER(20,5)|PULVERIZED COAL(16,5)|SWIRL VANE(16,4)|CEMENT CALCINATION NOX(16,1)|CEMENT DECARBOXYLATION(12,1)|COMBUSTION GAS(10,3)|REDUCING N O(10,1)|POLYAMIDE RESIN(9,2)|NONCATALYZED NOX REMOVAL(9,1)|MIXED FLOW(8,2)|STAGE CYCLONE(8,2)|LOWERMOST CYCLONE OUTLET GAS(8,1)|OXYGEN REGION(7,3)|CARBONYLDIAMIDE RESIN(7,2)|CYLINDRICAL MEMBER(6,5)|HEAVY OIL(6,4)|FIRE ZONE(6,1)|CEMENT CLINKER(5,2)|CEMENT RAW MATERIAL DECARBOXYLATION(5,2)|MEDIAN(5,2)|SWIRL ANGLE(5,2)|CHIMNEY EXHAUST GAS(5,1)|EXCESS AMMONIA(5,1)|MIXING AMMONIA(5,1)|NOX REMOVAL BAR(5,1)||(JPWO2015/133161)|CEMENT KILN(100,45)|EXHAUST GAS(100,21)|CEMENT KILN EXHAUST GAS(100,19)|NOX REMOVAL(100,15)|COMBUSTION AIR(100,12)|BURNER(100,11)|CEMENT(100,7)|CEMENT CALCINATION(100,6)|FUEL COMBUSTION(100,6)|KILN TAIL(100,6)|BLOWING FUEL(100,5)|CEMENT KILN TAIL(100,2)|CALCINING FURNACE(75,20)|COMBUSTIBLE WASTE(30,5)|KILN(26,15)|NOX(25,16)|NOX REMOVAL BURNER(18,13)|PULVERIZED COAL(16,6)|CARBONYLDIAMIDE(16,5)|CALCINING FURNACE BURNER(14,3)|CLINKER COOLER(13,5)|OXYGEN REGION(11,4)|CEMENT RAW MATERIAL DECARBOXYLATION(11,3)|SWIRL VANE(10,4)|CEMENT CALCINATION NOX(10,1)|MIXED FLOW(9,3)|BLADE(9,2)|HEAVY OIL(7,5)|CEMENT DECARBOXYLATION(7,1)|COMBUSTION GAS(6,3)|POLYAMIDE RESIN(6,2)|NONCATALYZED NOX REMOVAL(6,1)|REDUCING N O(6,1)|STAGE CYCLONE(5,2)|LOWERMOST CYCLONE OUTLET GAS(5,1)|CARBONYLDIAMIDE RESIN(4,2)|FIRE ZONE(4,1)|CYLINDRICAL MEMBER(3,5)|CEMENT CLINKER(3,2)|MEDIAN(3,2)|SWIRL ANGLE(3,2)|CHIMNEY EXHAUST GAS(3,1)|EXCESS AMMONIA(3,1)|MIXING AMMONIA(3,1)||(CN106029599)|CEMENT KILN(100,45)|EXHAUST GAS(100,20)|CEMENT KILN EXHAUST GAS(100,19)|DENITRATION(100,15)|CEMENT(100,11)|PREFIRING FURNACE(100,9)|PRECOMBUSTION FURNACE(54,3)|FUEL COMBUSTION(50,4)|FUEL BURNING(46,3)|COMBUSTIBLE WASTE(37,5)|NOX(31,18)|DENITRATION BURNER(29,12)|BLOWING FUEL(27,3)|FIRE(26,4)|BURNER(25,12)|RUNNING COST(21,1)|COMBUSTION AIR(20,15)|CARBONYLDIAMIDE(20,5)|FINE COAL(19,3)|COMBUSTOR(18,2)|ROTATING BLADE(16,4)|INLET END(14,14)|CEMENT RAW MATERIAL DECARBURIZATION(14,3)|PULVERIZED COAL(13,3)|SLAG COOLER(12,4)|FUEL SUPPLY(12,2)|NITROGEN OXIDE(11,1)|MIXED FLOW(10,4)|PREBURNING FURNACE BURNER(10,1)|HEAVY OIL(9,5)|COMBUSTION GAS(8,3)|ROTARY BLADE(7,3)|CLINKER COOLER(7,1)|CARBONYLDIAMIDE RESIN(6,2)|CALCINING FURNACE(6,1)|CEMENT BURNING(6,1)|ENTIRE CEMENT DECARBURIZATION(6,1)|LOWERMOST CYCLONE OUTLET GAS(6,1)|PREHEATER CYCLONE 2A(6,1)|REFRACTORY(5,3)|BURNING ZONE(5,1)|COOLING CEMENT CLINKER(5,1)|CYLINDRICAL MEMBER(4,5)|MEDIAN(4,2)|PREBURNER(4,2)|PREHEATER CONFIGURATION(4,1)|UNBURNED COMPONENT(4,1)||(IN334931)|CEMENT KILN(100,32)|EXHAUST GAS(100,16)|CEMENT(100,12)|DENITRIFYING CEMENT KILN(100,6)|CALCINING FURNACE(100,2)|DENITRATING EXHAUST GAS(100,2)|DENITRIFICATION BURNER(92,16)|KILN TAIL(92,3)|SWIRL VANE(40,8)|INFLAMMABLE WASTE(35,4)|COMBUSTION AIR(25,10)|NOX(25,10)|CEMENT RAW MATERIAL DECARBOCXYLATION(25,1)|CLINKER COOLER(19,4)|KILN INLET(18,7)|PULVERIZED COAL(18,5)|CALCINER BURNER(17,3)|INLET END(12,7)|PREHEATER CYCLONE 2A(12,2)|CHIMNEY RELEASING CEMENT KILN(11,1)|IV CATALYTIC DENITRIFICATION(11,1)|LOW OXYGEN ZONE(10,1)|RECOMBUSTING UNBURNT COMPONENT(10,1)|CEMENT KILN EXHAUST GAS(9,5)|MIXED FLOW(9,3)|REFRACTORY(8,4)|SWIRL ANGLE(8,4)|CARBONYLDIAMIDE RESIN(8,2)|DECREASING NOX(8,1)|CYLINDRICAL MEMBER(7,6)|HEAVY OIL(7,4)|CEMENT CLINKER(6,2)|OXYGEN REGION(6,2)|TERTIARY AIR(6,2)|BURNING ZONE(5,1)|DECREASE NOX(5,1)|EXCESS AMMONIA(5,1)|FUEL FL(5,1)||(IN201647033400)|CEMENT KILN(100,33)|EXHAUST GAS(100,17)|CEMENT(100,12)|DENITRIFYING CEMENT KILN(100,7)|DENITRATING EXHAUST GAS(100,1)|INFLAMMABLE WASTE(71,5)|BURNER(52,11)|DENITRIFICATION BURNER(45,14)|CALCINER(44,16)|CEMENT KILN EXHAUST GAS(43,7)|NOX(36,10)|PULVERIZED COAL(35,6)|SWIRL(34,4)|CEMENT RAW MATERIAL DECARBONATION(34,2)|BLADE(34,1)|COMBUSTION AIR(30,11)|OXYGEN REGION(29,3)|COMBUSTION(27,5)|KILN INLET(25,8)|SWIRL VANE(23,7)|CLINKER COOLER(20,4)|CALCINER BURNER(18,3)|INLET END(17,9)|HEAVY OIL(16,5)|NONCATALYTIC DENITRIFICATION(15,1)|CEMENT RAW MATERIAL(14,3)|SWIRLING FLOW(14,2)|PREHEATER CYCLONE 2A(12,2)|CHIMNEY RELEASING CEMENT KILN(12,1)|RECOMBUSTING UNBURNT COMPONENT(10,1)|REFRACTORY(9,4)|SWIRL ANGLE(9,4)|DECREASING NOX(9,1)|CARBONYLDIAMIDE RESIN(8,2)|CYLINDRICAL MEMBER(7,6)|CEMENT CLINKER(6,2)|TERTIARY AIR(6,2)|BURNING ZONE(6,1)|DECREASE NOX(6,1)|EXCESS AMMONIA(6,1)||(KR10-2016-0129842)|CEMENT KILN(100,43)|EXHAUST GAS(100,20)|CEMENT KILN EXHAUST GAS(100,17)|DENITRATION(100,13)|CEMENT(100,11)|CEMENT KILN TAIL(100,6)|KILN TAIL(68,19)|FUEL COMBUSTION(62,9)|FORMAT CALCINATION FURNACE(62,1)|CALCINATION FURNACE FORMAT(59,4)|CALCINING FURNACE(56,16)|BLOWING FUEL(52,2)|COMBUSTIBLE WASTE(32,5)|BURNER(25,20)|NOX(21,18)|COMBUSTION AIR(17,11)|PULVERIZED COAL(17,6)|DENITRATION BURNER(15,5)|CLINKER COOLER(13,5)|CEMENT RAW MATERIAL DECARBONATION(13,3)|FUEL SUPPLY(10,2)|NITROGEN OXIDE(10,1)|CALCINER BURNER(9,2)|FACTORY NOX ASSESSMENT(9,1)|HEAVY OIL(8,5)|MIXED FLOW(8,5)|SWIRL VANE(8,3)|CALCINING FURNACE BURNER(8,1)|CHIMNEY EMITTING CEMENT KILN(8,1)|COMBUSTION GAS(7,3)|CEMENT CALCINATION(7,1)|DENITRIFICATION BURNER(7,1)|POLYAMIDE RESIN(6,2)|CATALYTIC DENITRATION(6,1)|RECOMBUSTING UNCOMBUSTED COMPONENT(6,1)|REFRACTORY(5,4)|SWINGING BLADE(5,2)|UREA RESIN(5,2)|CALCINER FURNACE(5,1)|ENTIRE CEMENT DECARBONATION(5,1)|LOWERMOST CYCLONE OUTLET GAS(5,1)|CYLINDRICAL MEMBER(4,5)|CEMENT CLINKER(4,2)|FIRE(4,2)|MEDIAN(4,2)|SWING ANGLE(4,2)|CALCINATION TABLE(3,1)|EXCESS AMMONIA(3,1)|PREHEATER CONFIGURATION(3,1)|SWIRL STRENGTH(3,1)|LOW OXYGEN REGION(2,4)|ANGLE THETA(2,1)| (WO2015/133161)|1. A cement calcination device provided with a burner for combusting fuel by blowing fuel and combustion air into a kiln tail of a cement kiln.|2. The cement firing device according to claim 1, wherein the burner comprises swirling means for swirling a mixed flow of the fuel and the combustion air.|3. A method for NOx removal of cement kiln exhaust gas, comprising blowing fuel and combustion air into a kiln tail of a cement kiln to combust the fuel.|4. The method for NOx removal of cement kiln exhaust gas according to claim 3, wherein an amount of fuel supplied to the kiln tail of the cement kiln is not less than 20 % and less than 50 % of an amount of fuel supplied to a calcination furnace installed in the cement kiln.|5. The method for NOx removal of cement kiln exhaust gas according to claim 3 or 4, wherein the fuel supplied into the kiln tail of the cement kiln contains at least one of pulverized coal, heavy oil, and combustible waste. (WO2015/133161)|TECHNICAL FIELD|[0001] The present invention relates to a technique for reducing nitrogen oxide (hereinafter referred to as "NOx") concentration in a combustion gas discharged from a cement kiln.|BACKGROUND ART|[0002] The exhaust gas of the cement kiln contains NOx originating from the high-temperature region of the firing zone. when the concentration of NOx is high, a NOx removal agent such as urea or ammonia is introduced, or the NOx concentration is reduced by a reduction action of combustion in the calcination furnace. However, in a method using urea as a NOx removal agent, urea is expensive, and thus operation costs rise. In addition, when urea is added only, the NOx removal efficiency is low, and excess ammonia that has not reacted with NOx may be discharged to the outside of the system as is.|[0003] Patent Document 1 describes a method for reducing the NOx concentration of a cement calcination step by charging waste plastic containing a polyamide-based resin and a urea resin into a kiln end of a cement kiln and combusting the waste plastic, and mixing ammonia generated from the polyamide-based resin and urea generated from the urea resin with combustion gas to function as a non-catalyzed NOx removal agent.|[0004] Further, Patent Document 2 discloses a method of producing a calcined furnace in which a swirling strength of a swirling flow of the secondary air for combustion is adjusted to mix the secondary air containing a reducing gas and the kiln exhaust gas, and Described is a method of improving the NOx removal effect in the cement kiln exhaust gas by appropriately setting the position at which re-combustion air is supplied for re-combusting the uncombusted components remaining in the lower portion of the furnace body, and efficiently combusting the uncombusted components.|CITATION LIST|PATENT LITERATURE|[0005] PATENT CITATIONS|JP 5207474 a|JP 3768070 a|SUMMARY OF INVENTION|TECHNICAL PROBLEM|[0006] However, in the method described in Patent Document 1, the fired state in the cement firing apparatus deteriorates when waste plastic is fed to a kiln end having a low O2 concentration. Furthermore, in the method described in Patent Document 2, the form of the calcination furnace is limited, and thus, a calcination furnace of a different form from the calcination furnace described in the same document does not achieve a NOx removal effect.|[0007] Therefore, the present invention was conceived in view of the problems of the conventional technology described above, and an object of the present invention is to efficiently reduce the NOx concentration in the exhaust gas of the cement kiln while maintaining a favorable fired state regardless of the type of calcination furnace.|TECHNICAL SOLUTION|[0008] In order to achieve the object described above, the cement calcination device of the present invention is provided with a burner for blowing fuel and combustion air into the kiln tail of the cement kiln and combusting the fuel.|[0009] According to the cement calcination apparatus of the present invention, by providing the burner, it is possible to reduce NOx in the cement kiln exhaust gas in the low oxygen region in the kiln tail; It is also possible to improve the decarboxylation efficiency of the cement raw material by burning the fuel, and regardless of the type of calcination furnace, it is possible to efficiently reduce the NOx concentration in the cement kiln exhaust gas while maintaining a favorable calcined state.|[0010] In the cement calcination device described above, the burner can be provided with swirling means for swirling a mixed flow of the fuel and the combustion air. As a result, the combustion efficiency of the fuel is improved, and the decarboxylation efficiency can be further improved.|[0011] In addition, the present invention is a method for NOx removal of cement kiln exhaust gas, the method comprising blowing fuel and combustion air into the kiln tail of the cement kiln to combust the fuel. According to the present invention, it is possible to reduce the NOx in the cement kiln exhaust gas in the low oxygen region inside the kiln tail, improve the decarboxylation efficiency of the cement raw material, and efficiently reduce the NOx concentration in the cement kiln exhaust gas while maintaining a favorable fired state regardless of the type of calcination furnace.|[0012] In the above-described method for NOx removal of the cement kiln exhaust gas, the amount of fuel supplied to the kiln tail of the cement kiln may be set to 20 % or more and less than 50 % of the amount of fuel supplied to the calcination furnace attached to the cement kiln, and at least one of pulverized coal, heavy oil, and combustible waste may be included as the fuel.|ADVANTAGEOUS EFFECTS|[0013] As described above, according to the present invention, regardless of the type of calcination furnace, it is possible to efficiently reduce the NOx concentration in the cement kiln exhaust gas while maintaining a favorable firing state.|DESCRIPTION OF DRAWINGS|[0014] Fig.3 is a schematic view illustrating an embodiment of the cement kiln firing device according to the present invention. Shows the burner of Fig.1, where (a) is a cross-sectional view, (b) is a side view, and (c) is an expanded view of the burner tip.|DESCRIPTION OF EMBODIMENTS|[0015] Fig.1 illustrates an embodiment of a cement firing device according to the present invention. the cement firing device 1 includes: a pre-heater 2 that pre-heats a cement raw material (hereinafter referred to as "raw material") R; a calcination furnace 3 that calcined a raw material R1 from a cyclone 2 b in a third stage from the top of the pre-heater 2 using fuel F2 blown from a calcination furnace burner 13; A cement kiln 5 in which a raw material R2 from a lowermost cyclone 2 a of the pre-heater 2 is fired by fuel F1 blown in from a main burner 15; a clinker cooler 6 that cools the cement clinker fired in the cement kiln 5; a NOx removal burner 14 installed at a kiln end 4 of the cement kiln 5; and the like. Note that the configuration of the pre-heater 2, the calcination furnace 3, the cement kiln 5, the clinker cooler 6, and the like except for the NOx removal burner 14 are the same as those in the related art.|[0016] As illustrated in Fig.2, the NOx removal burner 14 is provided with a cylindrical member 14 h in which 6 ~ 10 swirler blades (swirler) 14 b are fixed at a swirl angle of 10 ~ 50 degrees to the tip of a cylindrical main body 14 a, a rod-like member 14 j positioned at the center of the cylindrical member 14 h, and a ring-shaped member 14 f positioned on the outer side of the tip of the cylindrical member 14 h. The NOx removal burner 14 is covered by refractory 14 e on the distal end side, and the mounting member 14 c on the rear end side of the main body 14 a and the surface 4 a of the kiln end 4 are joined by brackets 14 d to be mounted on the kiln end 4. The kiln tail 4 is also protected by the refractory 4 b. Note that, as illustrated in Fig. 2 (c), the swirl angle is the angle θ formed between the axial direction 14 m of the NOx removal burner 14 and the center line 14 g of the swirl vanes 14 b when the cylindrical member 14 h is unfolded flatly, and matches the swirl angle of the solid powder fuel flow F at the tip 14 k of the flow channel. The number and pivot angle of the swirl vanes 14 b can be appropriately changed.|[0017] Next, a method for NOx removal of cement kiln exhaust gas according to the present invention will be described with reference to FIGS.1 and 2.|[0018] The raw material R is preheated using the exhaust gas G from the cement kiln 5 in the preheater 2 of the cement firing device 1, and the raw material R1 from the cyclone 2 b of the preheater 2 is calcined in the calcining furnace 3. At this time, the tertiary air G1 from the clinker cooler 6 is blown in together with the fuel F2 from the calcination furnace burner 13 to combust the fuel F2. Pulverized coal, heavy oil, and the like are used as the fuel F2, and combustible waste may be used as part or all of the fuel F2.|[0019] The fuel F3 is also blown together with combustion air from a NOx removal burner 14 installed at the kiln end 4 of the cement kiln 5, and the fuel F3 is combusted. Pulverized coal, heavy oil, and combustible waste can be used as the fuel F3 in the same manner as the fuel F2 for the calcination furnace 3, and any one or more of these may be used simultaneously.|[0020] By blowing the fuel F3 from the NOx removal burner 14, NOx contained in the combustion gas G of the cement kiln 5 can be reduced in the low oxygen region in the kiln. Furthermore, by combusting the fuel F3 using combustion air, decarboxylation of the raw materials R2, R3 can be performed, and the decarboxylation efficiency of the overall cement firing device 1 can be improved. At this time, the flow of mixture of the fuel F3 and the combustion air is swirled by the swirler 14 b provided in the NOx removal burner 14 and blown into the kiln assembly 4, thereby improving the combustion efficiency of the fuel F3.|[0021] The ratio of the fuel F2 for the calcination furnace 3 and the fuel F3 blown from the NOx removal burner 14 is preferably adjusted to 20 % or more and less than 50 %. When the proportion of the fuel F3 is less than 20 %, the NOx removal effect is diminished, and when the proportion of the fuel F3 is greater than 50 %, the decarboxylation efficiency of the raw material R3 in the calcination furnace 3 is diminished, which is not preferable.|[0022] Next, fuel F1 such as pulverized coal is blown in from the main burner 15 of the cement kiln 5 to bake the raw material R2 from the cyclone 2 a of the pre-heater 2, and the obtained clinker is cooled by the clinker cooler 6 to obtain the cement clinker CL.|[0023] Next, a test example of a method for NOx removal of cement kiln exhaust gas using the cement firing device having the configuration described above will be described.|[0024] Table 1 shows the results of comparing the NOx concentrations of the outlet gas of the lowermost cyclone and the exhaust gas of the chimney that discharges the cement kiln exhaust gas to the atmosphere in three cement factories, between the case where the abovementioned NOx removal burner 14 was used (Working Example) and the case where the abovementioned NOx removal burner 14 was not used (Comparative Example).|[0025] |[0026] From this table, it can be seen that the NOx concentration at each evaluation position is reduced by using the NOx removal burner 14. In addition, although detailed data is omitted, in each of the examples described above, a favorable fired state is maintained in the cement kilns and the like, similar to the comparative examples.|[0027] Note that in the embodiment described above, the swirl vane 14 b is provided on the tip portion of the main body 14 a of the NOx removal burner 14, but this swirl vane 14 b is not necessarily required, and combustion air can be blown into the kiln end 4 together with the fuel F3 without swirling it.|REFERENCE SIGNS LIST|[0028] 1 Cement firing device 2 Preheater 2 a lowest stage cyclone 2 b third stage cyclone from top of top of 3 calcination furnace 4 kiln tail 4 a surface 4 b refractory material 5 cement kiln 6 clinker cooler 13 calcination furnace burner 14 NOx removal bar Donor 14 a Body 14 b swirl vane 14 c mounting member 14 d bracket 14 e refractory 14 f ring-shaped member 14 g centerline 14 h cylindrical member 14 j rod member 14 k tip of flow channel 14 m axial direction 15 main burner (WO2015/133161)|TECHNICAL FIELD|[0001] The present invention relates to a technique for reducing nitrogen oxide (hereinafter referred to as "NOx") concentration in a combustion gas discharged from a cement kiln.|BACKGROUND ART|[0002] The exhaust gas of the cement kiln contains NOx originating from the high-temperature region of the firing zone. when the concentration of NOx is high, a NOx removal agent such as urea or ammonia is introduced, or the NOx concentration is reduced by a reduction action of combustion in the calcination furnace. However, in a method using urea as a NOx removal agent, urea is expensive, and thus operation costs rise. In addition, when urea is added only, the NOx removal efficiency is low, and excess ammonia that has not reacted with NOx may be discharged to the outside of the system as is.|[0003] Patent Document 1 describes a method for reducing the NOx concentration of a cement calcination step by charging waste plastic containing a polyamide-based resin and a urea resin into a kiln end of a cement kiln and combusting the waste plastic, and mixing ammonia generated from the polyamide-based resin and urea generated from the urea resin with combustion gas to function as a non-catalyzed NOx removal agent.|[0004] Further, Patent Document 2 discloses a method of producing a calcined furnace in which a swirling strength of a swirling flow of the secondary air for combustion is adjusted to mix the secondary air containing a reducing gas and the kiln exhaust gas, and Described is a method of improving the NOx removal effect in the cement kiln exhaust gas by appropriately setting the position at which re-combustion air is supplied for re-combusting the uncombusted components remaining in the lower portion of the furnace body, and efficiently combusting the uncombusted components.|CITATION LIST|PATENT LITERATURE|[0005] PATENT CITATIONS|JP 5207474 a|JP 3768070 a|SUMMARY OF INVENTION|TECHNICAL PROBLEM|[0006] However, in the method described in Patent Document 1, the fired state in the cement firing apparatus deteriorates when waste plastic is fed to a kiln end having a low O2 concentration. Furthermore, in the method described in Patent Document 2, the form of the calcination furnace is limited, and thus, a calcination furnace of a different form from the calcination furnace described in the same document does not achieve a NOx removal effect.|[0007] Therefore, the present invention was conceived in view of the problems of the conventional technology described above, and an object of the present invention is to efficiently reduce the NOx concentration in the exhaust gas of the cement kiln while maintaining a favorable fired state regardless of the type of calcination furnace.|TECHNICAL SOLUTION|[0008] In order to achieve the object described above, the cement calcination device of the present invention is provided with a burner for blowing fuel and combustion air into the kiln tail of the cement kiln and combusting the fuel.|[0009] According to the cement calcination apparatus of the present invention, by providing the burner, it is possible to reduce NOx in the cement kiln exhaust gas in the low oxygen region in the kiln tail; It is also possible to improve the decarboxylation efficiency of the cement raw material by burning the fuel, and regardless of the type of calcination furnace, it is possible to efficiently reduce the NOx concentration in the cement kiln exhaust gas while maintaining a favorable calcined state.|[0010] In the cement calcination device described above, the burner can be provided with swirling means for swirling a mixed flow of the fuel and the combustion air. As a result, the combustion efficiency of the fuel is improved, and the decarboxylation efficiency can be further improved.|[0011] In addition, the present invention is a method for NOx removal of cement kiln exhaust gas, the method comprising blowing fuel and combustion air into the kiln tail of the cement kiln to combust the fuel. According to the present invention, it is possible to reduce the NOx in the cement kiln exhaust gas in the low oxygen region inside the kiln tail, improve the decarboxylation efficiency of the cement raw material, and efficiently reduce the NOx concentration in the cement kiln exhaust gas while maintaining a favorable fired state regardless of the type of calcination furnace.|[0012] In the above-described method for NOx removal of the cement kiln exhaust gas, the amount of fuel supplied to the kiln tail of the cement kiln may be set to 20 % or more and less than 50 % of the amount of fuel supplied to the calcination furnace attached to the cement kiln, and at least one of pulverized coal, heavy oil, and combustible waste may be included as the fuel.|ADVANTAGEOUS EFFECTS|[0013] As described above, according to the present invention, regardless of the type of calcination furnace, it is possible to efficiently reduce the NOx concentration in the cement kiln exhaust gas while maintaining a favorable firing state.|DESCRIPTION OF DRAWINGS|[0014] Fig.3 is a schematic view illustrating an embodiment of the cement kiln firing device according to the present invention. Shows the burner of Fig.1, where (a) is a cross-sectional view, (b) is a side view, and (c) is an expanded view of the burner tip.|DESCRIPTION OF EMBODIMENTS|[0015] Fig.1 illustrates an embodiment of a cement firing device according to the present invention. the cement firing device 1 includes: a pre-heater 2 that pre-heats a cement raw material (hereinafter referred to as "raw material") R; a calcination furnace 3 that calcined a raw material R1 from a cyclone 2 b in a third stage from the top of the pre-heater 2 using fuel F2 blown from a calcination furnace burner 13; A cement kiln 5 in which a raw material R2 from a lowermost cyclone 2 a of the pre-heater 2 is fired by fuel F1 blown in from a main burner 15; a clinker cooler 6 that cools the cement clinker fired in the cement kiln 5; a NOx removal burner 14 installed at a kiln end 4 of the cement kiln 5; and the like. Note that the configuration of the pre-heater 2, the calcination furnace 3, the cement kiln 5, the clinker cooler 6, and the like except for the NOx removal burner 14 are the same as those in the related art.|[0016] As illustrated in Fig.2, the NOx removal burner 14 is provided with a cylindrical member 14 h in which 6 ~ 10 swirler blades (swirler) 14 b are fixed at a swirl angle of 10 ~ 50 degrees to the tip of a cylindrical main body 14 a, a rod-like member 14 j positioned at the center of the cylindrical member 14 h, and a ring-shaped member 14 f positioned on the outer side of the tip of the cylindrical member 14 h. The NOx removal burner 14 is covered by refractory 14 e on the distal end side, and the mounting member 14 c on the rear end side of the main body 14 a and the surface 4 a of the kiln end 4 are joined by brackets 14 d to be mounted on the kiln end 4. The kiln tail 4 is also protected by the refractory 4 b. Note that, as illustrated in Fig. 2 (c), the swirl angle is the angle θ formed between the axial direction 14 m of the NOx removal burner 14 and the center line 14 g of the swirl vanes 14 b when the cylindrical member 14 h is unfolded flatly, and matches the swirl angle of the solid powder fuel flow F at the tip 14 k of the flow channel. The number and pivot angle of the swirl vanes 14 b can be appropriately changed.|[0017] Next, a method for NOx removal of cement kiln exhaust gas according to the present invention will be described with reference to FIGS.1 and 2.|[0018] The raw material R is preheated using the exhaust gas G from the cement kiln 5 in the preheater 2 of the cement firing device 1, and the raw material R1 from the cyclone 2 b of the preheater 2 is calcined in the calcining furnace 3. At this time, the tertiary air G1 from the clinker cooler 6 is blown in together with the fuel F2 from the calcination furnace burner 13 to combust the fuel F2. Pulverized coal, heavy oil, and the like are used as the fuel F2, and combustible waste may be used as part or all of the fuel F2.|[0019] The fuel F3 is also blown together with combustion air from a NOx removal burner 14 installed at the kiln end 4 of the cement kiln 5, and the fuel F3 is combusted. Pulverized coal, heavy oil, and combustible waste can be used as the fuel F3 in the same manner as the fuel F2 for the calcination furnace 3, and any one or more of these may be used simultaneously.|[0020] By blowing the fuel F3 from the NOx removal burner 14, NOx contained in the combustion gas G of the cement kiln 5 can be reduced in the low oxygen region in the kiln. Furthermore, by combusting the fuel F3 using combustion air, decarboxylation of the raw materials R2, R3 can be performed, and the decarboxylation efficiency of the overall cement firing device 1 can be improved. At this time, the flow of mixture of the fuel F3 and the combustion air is swirled by the swirler 14 b provided in the NOx removal burner 14 and blown into the kiln assembly 4, thereby improving the combustion efficiency of the fuel F3.|[0021] The ratio of the fuel F2 for the calcination furnace 3 and the fuel F3 blown from the NOx removal burner 14 is preferably adjusted to 20 % or more and less than 50 %. When the proportion of the fuel F3 is less than 20 %, the NOx removal effect is diminished, and when the proportion of the fuel F3 is greater than 50 %, the decarboxylation efficiency of the raw material R3 in the calcination furnace 3 is diminished, which is not preferable.|[0022] Next, fuel F1 such as pulverized coal is blown in from the main burner 15 of the cement kiln 5 to bake the raw material R2 from the cyclone 2 a of the pre-heater 2, and the obtained clinker is cooled by the clinker cooler 6 to obtain the cement clinker CL.|[0023] Next, a test example of a method for NOx removal of cement kiln exhaust gas using the cement firing device having the configuration described above will be described.|[0024] Table 1 shows the results of comparing the NOx concentrations of the outlet gas of the lowermost cyclone and the exhaust gas of the chimney that discharges the cement kiln exhaust gas to the atmosphere in three cement factories, between the case where the abovementioned NOx removal burner 14 was used (Working Example) and the case where the abovementioned NOx removal burner 14 was not used (Comparative Example).|[0025] |[0026] From this table, it can be seen that the NOx concentration at each evaluation position is reduced by using the NOx removal burner 14. In addition, although detailed data is omitted, in each of the examples described above, a favorable fired state is maintained in the cement kilns and the like, similar to the comparative examples.|[0027] Note that in the embodiment described above, the swirl vane 14 b is provided on the tip portion of the main body 14 a of the NOx removal burner 14, but this swirl vane 14 b is not necessarily required, and combustion air can be blown into the kiln end 4 together with the fuel F3 without swirling it.|REFERENCE SIGNS LIST|[0028] 1 Cement firing device 2 Preheater 2 a lowest stage cyclone 2 b third stage cyclone from top of top of 3 calcination furnace 4 kiln tail 4 a surface 4 b refractory material 5 cement kiln 6 clinker cooler 13 calcination furnace burner 14 NOx removal bar Donor 14 a Body 14 b swirl vane 14 c mounting member 14 d bracket 14 e refractory 14 f ring-shaped member 14 g centerline 14 h cylindrical member 14 j rod member 14 k tip of flow channel 14 m axial direction 15 main burner Family Number|(70851444)|70851444|Abstract|(TH-166474 A)|To effectively reduce NOx concentrations in the exhaust from cement kilns while maintaining a favorite combustion condition regardless of the type of calciner, the machine for burning 1 cement that includes 14 burners for blowing F3 fuel and air from combustion. Towards the end of the inlet 4 of the 5 cement kiln to burn the NOx fuel in the exhaust from the cement kiln can be reduced in the low oxygen area at the end of the furnace inlet, and the fuel burning improves the carbon removal efficiency of the cement raw materials with the head. A burner can include 14b rotary blade (rotary pathway) for rotating the flow, where the fuel and air from the combustion are mixed. Ideally, the amount of fuel that has been blown to the inlet end of the furnace. Cement is equal to or greater than 20% and less than 50% of the amount. The fuel that has been blown to the calciners that have been attached to the cement kiln and the fuel that has been blown to the inlet end of the cement kiln may include at least one of the crushed coal, heavy oil and flammable waste.|CPC codes|(WO2015133161 A1)|B01D-053/00/5|B01D-053/56|(CN106029599 A)|B01D - 053/00/5 |B01D - 053/56 |(KR20160129842 A)|B01D-053/00/5|B01D-053/56|(JP6476165 B2)|B01D-053/00/5|B01D-053/56|(MY-183200 A)|B01D-053/00/5|B01D-053/56|IPC codes|(WO2015133161 A1)|B01D-053/56|(CN106029599 A)|B01D - 053/56 |(KR20160129842 A)|B01D-053/00|B01D-053/56|(IN-334931 B)|B01D-053/56|(JP6476165 B2)|B01D-053/56|B01D-053/76|(ID201710506 A)|B01D-053/56| Environmental technology|Materials, metallurgy B01D-053/00/5|B01D-053/56|C04B-007/36/4|C04B-007/44|F27B-007/34|F27D-099/00/33 B01D-053/00/5|B01D-053/56|C04B-007/36/4|C04B-007/44|F27B-007/34|F27D-099/00/33 B01D-053/00|B01D-053/56|B01D-053/76|C04B-007/36|C04B-007/44|C04B-007/60 B01D-053/00|B01D-053/56|B01D-053/76|C04B-007/36|C04B-007/44|C04B-007/60 JP2018025482W|CN112601725|JP2021019753W;JP2021019753W|WO202119753|WO201825482|JP2023145046W;JP2023145046W|EP3998425;EP3998425;EP3998425|KR20210018176|KR20210018176|US12196417|WO202124386|KR20210015601|JP2020193115|CN111514726B|TWI667061 JP2018025482W 76877034 WHO=Examiner SELF=Y CAT=Y|CN112601725 92570633 WHO=Examiner SELF=Y CAT=A|JP2021019753W 92570633 WHO=Examiner SELF=Y CAT=A|WO202119753 92570633 WHO=Examiner SELF=Y CAT=A|WO201825482 76877034 WHO=Examiner SELF=Y CAT=A|JP2023145046W 105974964 WHO=Examiner SELF=Y|EP3998425 92704796 WHO=Applicant SELF=Y|KR20210018176 92704796 WHO=Examiner SELF=Y|KR20210018176 92704796 WHO=Applicant SELF=Y|US12196417 92704796 WHO=Applicant SELF=Y|WO202124386 92704796 WHO=Applicant SELF=Y|KR20210015601 92570633 WHO=Applicant SELF=Y|JP2020193115 91745622 WHO=Applicant SELF=N|CN111514726B 90149469 WHO=Examiner SELF=N|TWI667061 85547095 WHO=Examiner SELF=N CN103591578|JP2008222504|JP2006298685|CN102923979|JP61068129|JP58202033|CN102923979|JP4647375|JP60137857|JP84038015|CN102923979|JP5207474|JP2008222504|JP2006298685|JP3768070|JP3768070|JP05207474|JP61068129|JP60137857|JP58202033|JP58202033 CN103591578 61783596 WHO=Examiner SELF=N CAT=Y|JP2008222504 22897637 WHO=Examiner SELF=N CAT=Y|JP2006298685 22654225 WHO=Examiner SELF=N CAT=Y|CN102923979 8098760 WHO=Examiner SELF=N CAT=X CAT=Y|JP61068129 27160271 WHO=Examiner SELF=N CAT=X CAT=Y|JP58202033 26797017 WHO=Examiner SELF=N CAT=X CAT=Y|CN102923979 8098760 WHO=Examiner SELF=N CAT=A|JP4647375 22654225 WHO=Examiner SELF=N CAT=A|JP60137857 23832698 WHO=Examiner SELF=N CAT=A|JP84038015 26797017 WHO=Examiner SELF=N CAT=A|CN102923979 8098760 WHO=Examiner SELF=N|JP5207474 33219042 WHO=Applicant SELF=N|JP2008222504 22897637 WHO=Examiner SELF=N|JP2006298685 22654225 WHO=Examiner SELF=N|JP3768070 22072574 WHO=Applicant SELF=N|JP3768070 22072574 WHO=Applicant SELF=N|JP05207474 28307388 WHO=Applicant SELF=N|JP61068129 27160271 WHO=Examiner SELF=N|JP60137857 23832698 WHO=Examiner SELF=N|JP58202033 26797017 WHO=Examiner SELF=N|JP58202033 26797017 WHO=Unknown SELF=N 日本国特許第5207474号公報|日本国特許第3768070号公報|特開昭58−202033(JP,A)|特開昭61−068129(JP,A)|中国特許出願公開第102923979(CN,A)|特開2006−298685(JP,A)|特開2008−222504(JP,A)|特開昭60−137857(JP,A)|朱永礼等: &quot;低氮分级燃烧技术在10000t/d生产线上的应用实践&quot;, 《水泥》 (Cat. Y,X) JP58202033; JP61068129; CN102923979; JP2006298685; JP2008222504; JP60137857|||JP58202033; JP61068129; CN102923979; JP2006298685; JP2008222504; JP60137857; JP5207474; JP3768070|JP58202033||JP05207474; JP3768070|JP84038015; JP4647375; CN102923979; CN103591578 GRANTED (WO2015/133161)|LAPSED|(JP6476165)|LAPSED|(CN106029599)|REVOKED|(MY183200)|GRANTED|(IN334931)|GRANTED|(ID2017/10506)|LAPSED|(TH166474)|LAPSED|(KR10-2016-0129842)|REVOKED ALIVE (WO2015/133161)|DEAD|(JP6476165)|DEAD|(CN106029599)|DEAD|(MY183200)|ALIVE|(IN334931)|ALIVE|(ID2017/10506)|DEAD|(TH166474)|DEAD|(KR10-2016-0129842)|DEAD (WO2015/133161)|LEGAL DETAILS FOR WO2015/133161|Actual or expected expiration date=2017-09-06|Legal state=DEAD|Status=LAPSED|Event publication date=2015-01-08|Event code=WO/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=WO WOJP2015/050310|Application date=2015-01-08|Standardized application number=2015WO-JP50310|Event publication date=2015-09-11|Event 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reason for refusal|Event publication date=2021-10-25|Event code=KR/E601|Event indicator=Neg|Event group=Event indicating Not In Force|Decision to refuse application (WO2015/133161)|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW|(WO2015/133161)|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ|(WO2015/133161)|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR|(WO2015/133161)|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML|(WO2015/133161)|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IR, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL (WO2015/133161)|IN; MY|(MY183200)|MY|(IN334931)|IN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCCwO5hgBc7WTN0P/F2Pwh1EkaV0SMUACwOCCKReMmHu7M9Ry4MrhQjLALkMBz8hwaI=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO2015133161&ekey=1194&xpn=WO2015133161&kind=A1 http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2015133161&redirectedID=true https://permalink.orbit.com/RenderStaticFirstPage?XPN=ychBnXNZRz%252BnZQVwANGCHbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT JP (WO2015/133161)|JP (WO2015/133161)|NAME=TAIHEIYO ENGINEERING CORPORATION ST Nishikasai Building, 4th Floor, 8-4-6, Nishikasai, Edogawa-ku, Tokyo 1340088 , COUNTRY=JP (WO2015/133161)|JP||||| (WO2015/133161)|NAME=NAKAI Jun 2nd Floor, Ezawa Building, 10-8, Shinjuku 5-chome, Shinjuku-ku, Tokyo 1600022 , POSTCODE=〒1600022 , COUNTRY=JP|(JP6476165)|NAME=NAKAI, Jun , REG=100106563|(CN106029599)|NAME=WANG YONGHONG;CCPIT PATENT & TRADEMARK LAW OFFICE , REG=11038|(ID2017/10506)|NAME=Dora Am Badar S Psi|(TH166474)|NAME=Mr. Chakrapit Mongkolsit, Miss Jaiyot Srikitjaaporn, Mr. Ruth Nopkhun|(KR10-2016-0129842)|NAME=Y.S.CHANG & ASSOCIATES , REG=920171002811 (WO2015/133161)|JP||||||||| (WO2015/133161)|NAME=SUZUKI Hideto c/o TAIHEIYO ENGINEERING CORPORATION, ST Nishikasai Building, 4th Floor, 8-4-6, Nishikasai, Edogawa-ku, Tokyo 1340088, POSTCODE=〒1340088, COUNTRY=JP|(JP6476165)|NAME=SUZUKI Hideto|(JPWO2015/133161)|NAME=SUZUKI Hideto|(CN106029599)|NAME=SUZUKI HIDETO|(MY183200)|NAME=SUZUKI Hideto|(IN334931)|NAME=Suzuki Hideto|(IN201647033400)|NAME=SUZUKI Hideto|(ID2017/10506)|NAME=Hideto SUZUKI|(TH166474)|NAME=Suzuki|NAME=Hideo|(KR10-2016-0129842)|NAME=SUZUKI HIDETO 21 8 Titre: (WO2015/133161)|Cement burning apparatus, and method for denitrating exhaust gas from cement kiln Résumé: (WO2015/133161)|[Problem] To efficiently reduce the concentration of NOx in an exhaust gas from a cement kiln while keeping the burned state at a good level regardless of the type of a calcining furnace to be used. [Solution] A cement burning apparatus (1) equipped with a burner (14) for blowing a fuel (F3) and combustion air into a kiln tail part (4) of a cement kiln (5) to burn the fuel. It becomes possible to reduce NOx, which is contained in an exhaust gas from the cement kiln, in a low-oxygen zone in the kiln tail part, and it also becomes possible to improve the decarbocxylation efficiency of a cement raw material due to the burning of the fuel. The burner may be equipped with a swirl vane (a swirl means) (14b) for swirling a mixed flow of the fuel and the combustion air. It is preferred that the amount of the fuel to be supplied into the kiln tail part of the cement kiln is 20% or more and less than 50% of the amount of the fuel to be supplied into a calcining furnace (3) that is provided in the cement kiln. The fuel to be supplied into the kiln tail part of the cement kiln may comprise at least one of pulverized coal, a heavy oil and a burnable waste material. 126 Abstract gpt-4o-mini no The article focuses on reducing NOx emissions from a cement kiln and does not address accelerated weathering or CO2 capture.
127 CN202510370583 CN202510370583 CN120188688 115012249 CN120188688 A 2025-06-24 [CN120188688] 2025-03-27 2025-03-27 2025-06-24 (CN120188688)|2045-03-27 (CN120188688)|Method for promoting growth of coastal wetland scirpus mariqueter by using spartina alterniflora charcoal (CN120188688)|The invention discloses a method for promoting the growth of coastal wetland scirpus mariqueter by using spartina alterniflora biochar, which comprises the following steps: S1, collecting spartina alterniflora, cleaning, naturally airing, cutting into small sections of less than 5 cm, drying at 60 DEG C, crushing, sieving by a 60-mesh sieve, and performing anaerobic pyrolysis at 500 DEG C for 2 hours to prepare biochar; s2, coast wetland salt marsh soil is collected, 0%, 0.5%, 1% and 3% of biochar are added according to the weight ratio, and the biochar and the soil are mixed to be uniform to prepare different treatment groups; s3, healthy scirpus mariqueter seedlings are selected, transplanted into the soil containing the biochar and cultured for 9 months under the greenhouse condition; s4, regularly measuring plant biomass, root morphology, reproduction characteristics and soil indexes, and finally screening 1% biochar addition concentration as an optimal scheme; according to the method, resource utilization of invasive plants is achieved, the wetland carbon sequestration potential is enhanced, and a scientific basis and an application approach are provided for coastal wetland ecological restoration and blue carbon sink management. RESEARCH INSTITUTE OF SUBTROPICAL FORESTRY CHINESE ACADEMY OF FORESTRY (CN120188688)|RESEARCH INSTITUTE OF SUBTROPICAL FORESTRY CHINESE ACADEMY OF FORESTRY ([CN]) LI NIU|WU MING|SHAO XUEXIN|TANG YAOYAO|JIANG PENGCHENG|GAO JINGWEN (CN120188688)|LI NIU|WU MING|SHAO XUEXIN|TANG YAOYAO|JIANG PENGCHENG|GAO JINGWEN (CN120188688)|LIU HUIMIN;BEIJING JUNTAI-MIZUKI INTELLECTUAL PROPERTY AGENCY LTD.|Reg. Nb: 11906 (CN120188688)|However, its growth and propagation are limited by the supply of soil nutrients and physicochemical properties.|However, its growth is limited by soil nutrients and physicochemical properties.| (CN120188688)|1. The method for promoting the growth of the spartina alterniflora by utilizing the spartina alterniflora biochar is characterized by comprising the following steps of: S1, preparing biochar, namely collecting spartina alterniflora, naturally airing after cleaning, cutting into small sections below 5 cm, drying at 60 ℃, crushing by using a crusher, sieving by using a 60-mesh sieve, and performing anaerobic pyrolysis at 500 ℃ for 2 hours to prepare the biochar; S2, soil treatment, namely collecting coastal wetland salt swamp soil, adding 0%, 0.5%, 1% and 3% of biochar according to the weight ratio, and fully and uniformly mixing with the soil to prepare different treatment groups; S3, planting plants, namely selecting healthy scirpus seedlings, transplanting the scirpus seedlings into soil containing biochar, planting 24 plants in each container, keeping the soil moisture to be about 60% of the field water holding capacity, watering twice a week, and culturing for 9 months under the greenhouse condition; and S4, growth management, namely periodically measuring plant biomass, root system morphology, propagation characteristics and soil indexes, and finally screening the 1% biochar adding concentration as the optimal scheme. | (CN120188688)|The invention discloses a method for promoting the growth of seashore wet scirpus by utilizing spartina alterniflora biochar, which comprises the following steps of S1, collecting spartina alterniflora, naturally airing, cutting into small sections below 5 cm ℃, crushing after 60 ℃ drying, sieving with a 60-mesh sieve, carrying out anaerobic pyrolysis at 500 ℃ for 2 hours to prepare biochar, S2, collecting seashore wet salt marsh soil, adding 0%, 0.5%, 1% and 3% of biochar according to the weight ratio, uniformly mixing with soil to prepare different treatment groups, S3, selecting healthy spartina alterniflora seedlings, transplanting into soil containing the biochar, and culturing for 9 months under a greenhouse condition, S4, periodically measuring plant biomass, root morphology, propagation characteristics and soil indexes, and finally screening 1% of biochar addition concentration as an optimal scheme, and realizing the utilization of invasive plant resources, enhancing the carbon fixing potential of the seashore wet ecological restoration and blue carbon assembly management.|The invention relates to the technical field of wetland ecology and carbon circulation, in particular to a method for promoting the growth of scirpus maritima in a coastal wetland by utilizing spartina alterniflora biochar, which is suitable for the ecological restoration of the coastal wetland, the resource utilization of invasive plants and the improvement of carbon sink functions.|The present invention is intended to embrace all such alternatives, modifications and variances which fall within the broad scope of the appended claims.| (CN120188688)|SPARTINA ALTERNIFLORA(100,24)|GROWTH PROMOTION(100,15)|SPARTINA ALTERNIFLORA BIOCHAR(100,7)|SPARTINA ALTERNIFLORA PROMOTING GROWTH(100,1)|HEALTHY SPARTINA ALTERNIFLORA SEEDLING(96,1)|SEASHORE WET ECOLOGICAL RESTORATION(73,1)|SEASHORE WET SCIRPUS(71,1)|HEALTHY SCIRPUS ACULEATUS SEEDLING(69,1)|SPARTINA ALTERNIFLORA SEEDLING(67,1)|COASTAL WETLAND SPARGANIUM STOLONIFER(62,1)|COASTAL WETLAND SPARTINA ALTERNIFLORA(60,2)|COASTAL WETLAND SCIRPUS ACULEATUS(60,1)|COLLECTING SPARTINA ALTERNIFLORA(59,5)|COLLECTING SEASHORE WET(58,1)|TRANSPLANTING SCIRPUS ACULEATUS(58,1)|INVASIVE PLANT RESOURCE UTILIZATION(55,7)|ANAEROBIC PYROLYSIS(55,5)|HEALTHY SCIRPUS SEEDLING(54,4)|PERIODICALLY MEASURING PLANT BIOMASS(53,1)|COASTAL WETLAND ECOLOGICAL RESTORATION(49,5)|PLANT BIOMASS(48,6)|WETLAND ECOLOGY(45,1)|WET ECOLOGICAL RESTORATION(43,1)|COASTAL WETLAND(42,18)|BIOCHAR(41,16)|SOIL INDEX(41,5)|SCIRPUS SEEDLING(40,3)|INVASIVE PLANT RESOURCE(40,1)|TOTAL SCIRPUS ACULEATUS BIOMASS(35,1)|ABOVEGROUND BIOMASS(34,1)|GREENHOUSE CONDITION(33,6)|RESOURCE UTILIZATION(33,4)|COASTAL WETLAND SALT SWAMP(31,3)|COLLECTED COASTAL WETLAND DEPTH(29,1)|PLANTING PLANT(27,3)|GROUND(26,13)|PHYSICOCHEMICAL PROPERTY(25,2)|UNDERGROUND BIOMASS(24,4)|SALT MARSH LAND(24,3)|SOIL NUTRIENT(23,5)|CARBON CIRCULATION(23,1)|ECOLOGICAL RESTORATION(19,7)|SOIL TREATMENT(19,3)|BLUE CARBON ASSEMBLY MANAGEMENT(19,1)|AMMONIUM NITROGEN(18,6)|SOIL NITRATE(18,3)|MORPHOLOGY(18,2)|ILLUMINATION INTENSITY(17,3)|AIRING(17,2)|BIOCHAR ADDITION(16,4)|PROPAGATION(16,1)|INVASIVE PLANT(15,4)|PLANTING(15,3)|WEIGHT RATIO(15,3)|TRANSPLANTING SCIRPUS MARITIMA SEEDLING(15,1)|CRUSHER(14,4)|NITRATE NITROGEN(14,4)|CARBON FIXING(13,1)|PHOSPHORUS AVAILABILITY(12,7)|SCIRPUS(12,5)|SOIL MOISTURE(12,3)|GROWTH MANAGEMENT(12,2)|60 MESH SIEVE(11,5)|NITRIFICATION RATE(11,4)|ROOT SYSTEM MORPHOLOGY(11,3)|SALT SWAMP(11,3)|ROOT VOLUME(10,3)|SALINITY(10,3)|CARBON SINK(10,1)|TREATMENT GROUP(9,5)|HUMIDITY(9,4)|CARBON SINK FUNCTION(9,1)|MU MOL(8,4)|NUTRIENT AVAILABILITY(8,3)|BROAD SCOPE(8,1)|HEALTHY SCIRPUS SEEDLING HEIGHT(8,1)|SCIRPUS ACULEATUS GROWTH(8,1)|TOTAL NITROGEN(7,3)|COASTAL WETLAND ECOSYSTEM(7,1)|SPARTINA ALTERNIFLORA DENSE GROWTH(7,1)|SPARTINA ALTERNIFLORA INVASION(7,1)|ROOT LENGTH(6,5)|TOTAL CARBON(6,3)|FOOD RESOURCE(6,2)|SCIRPUS TOTAL BIOMASS(6,2)|WETLAND CARBON RESERVE LOSS(6,2)|COASTAL WETLAND RESTORATION(6,1)|COASTAL WETLAND SOIL(6,1)|PYROLYTIC BIOCHAR(6,1)|RECOVERING COASTAL WETLAND(6,1)|SMALL SECTION(5,5)|ROOT DEVELOPMENT(5,3)|BIOCHAR TREATMENT(5,2)|CONCENTRATION DEPENDENCY(5,2)|PLANT PROPAGATION STRATEGY(5,2)|KEY BIOLOGICAL HABITAT(5,1)|PERENNIAL HERBACEOUS PLANT(5,1)|VEGETATION COMMUNITY DEGRADATION(5,1)|CARBON FIXATION CAPACITY(4,3)|ORGANIC CARBON(4,3)|SIGNIFICANCE(4,3)|SOIL ENVIRONMENT(4,2)|BIODIVERSITY BALANCE(4,1)|CARBON WAREHOUSE(4,1)|CLIMATE REGULATION(4,1)|COASTAL ECONOMIC ACTIVITY(4,1)|COMPACT GROWTH(4,1)|EARTH ENVIRONS OPTIMIZATION(4,1)|ECOLOGICAL BENEFIT(4,1)|ECOLOGICAL RESTORATION DEVELOPMENT(4,1)|ENVIRONMENT ADAPTABILITY(4,1)|GLOBALLY IMPORTANT ECOSYSTEM(4,1)|GROUND OPTIMIZATION(4,1)|GROWING MANAGEMENT(4,1)|NATIVE PLANT RESTORATION(4,1)|RESOURCE CIRCULATION(4,1)|SALT ACCUMULATION AVOIDANCE(4,1)|TECHNOLOGICAL PARAMETER(4,1)|WETLAND CARBON SEQUESTRATION CAPACITY(4,1)| (CN120188688)|1. The method for promoting the growth of the spartina alterniflora by utilizing the spartina alterniflora biochar is characterized by comprising the following steps of:| S1, preparing biochar, namely collecting spartina alterniflora, naturally airing after cleaning, cutting into small sections below 5 cm, drying at 60 ℃, crushing by using a crusher, sieving by using a 60-mesh sieve, and performing anaerobic pyrolysis at 500 ℃ for 2 hours to prepare the biochar; |S2, soil treatment, namely collecting coastal wetland salt swamp soil, adding 0%, 0.5%, 1% and 3% of biochar according to the weight ratio, and fully and uniformly mixing with the soil to prepare different treatment groups; | S3, planting plants, namely selecting healthy scirpus seedlings, transplanting the scirpus seedlings into soil containing biochar, planting 24 plants in each container, keeping the soil moisture to be about 60% of the field water holding capacity, watering twice a week, and culturing for 9 months under the greenhouse condition; | and S4, growth management, namely periodically measuring plant biomass, root system morphology, propagation characteristics and soil indexes, and finally screening the 1% biochar adding concentration as the optimal scheme. |2. The method for promoting the growth of the coastal wetland sparganium stolonifer using sparganium stolonifer biochar according to claim 1, wherein in the step S2, the depth of the collected coastal wetland salt marsh is 0-10cm.|3. The method for promoting the growth of scirpus aculeatus in coastal wetland by using spartina alterniflora biochar according to claim 1, wherein in the step S3, the height of the healthy scirpus aculeatus seedlings is 10-15cm, the root system is complete, and the size of the container for transplanting scirpus aculeatus is 55cm x 40cm x 35cm.|4. The method for promoting the growth of the coastal wetland spartina alterniflora by utilizing spartina alterniflora biochar according to claim 3, wherein in the step S3, the greenhouse condition is that the temperature is 25-30 ℃, the illumination intensity is 500 mu mol m -2 s-1, and the humidity is 60-70%.|5. The method for promoting the growth of the coastal wetland spartina alterniflora according to claim 1, wherein in the step S4, the plant biomass comprises the ground and the underground, the root system morphology comprises root length, root surface area and root volume, the propagation characteristics comprise seed number and bulb number, and the soil indexes comprise water content, pH, salinity, conductivity, nitrate nitrogen, ammonium nitrogen, available phosphorus, total nitrogen, total carbon and organic carbon.|6. The method for promoting the growth of the coastal wetland scirpus aculeatus by using spartina alterniflora biochar according to claim 5, wherein the 1% biochar addition concentration increases the total scirpus aculeatus biomass by 35%, the aboveground biomass by 36.65%, the underground biomass by 115.04%, the root length by 135.84%, the soil nitrate nitrogen by 14.35%, the ammonium nitrogen by 26.84%, the available phosphorus by 20.15%, and the soil nutrient and nitrification rate are remarkably optimized for the optimal concentration.|7. The method for promoting the growth of the spartina alterniflora by utilizing the spartina alterniflora biochar according to claim 1, which is characterized by being suitable for ecological restoration of the coastal wetland, resource utilization of invasive plants and blue carbon sink management. (CN120188688)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of wetland ecology and carbon circulation, in particular to a method for promoting the growth of scirpus maritima in a coastal wetland by utilizing spartina alterniflora biochar, which is suitable for the ecological restoration of the coastal wetland, the resource utilization of invasive plants and the improvement of carbon sink functions.|BACKGROUND ART|[0002] Coastal wetlands are globally important ecosystems with the functions of maintaining biodiversity, regulating climate and storing "blue carbon". However, the invasion of spartina alterniflora has a versatile negative impact on the ecosystem. The rapid diffusion of the plant growth regulator is used for occupying the living space of the original plants, so that the degradation of the original vegetation community is caused, and the balance of biodiversity is destroyed. In addition, the dense growth of the spartina alterniflora also causes the blockage of a channel, influences water traffic and coastal economic activities, and threatens the health and functions of the coastal wetland ecosystem. The existing treatment method mostly adopts mechanical cleaning, but the situation is broken and the carbon warehouse is lost, so that the carbon fixing capacity of the wetland is weakened. Natural-based solutions are considered as effective ways to reestablish the ecological function of the wetland by native plant restoration and soil improvement.|[0003] The scirpus maritima is an ideal species for recovering the coastal wetland, and has remarkable significance for maintaining biodiversity and protecting key biological habitat due to the strong environment adaptability and the characteristic of being an important food resource of birds. However, its growth is limited by soil nutrients and physicochemical properties. The biochar is used as a soil conditioner, can improve the soil environment and promote plant growth, but the prior research has not systematically revealed the concentration dependency effect and carbon fixation mechanism of spartina alterniflora biochar on scirpus. Therefore, the development of the ecological restoration technology based on spartina alterniflora biochar has important significance.|[0004] The scirpus maritimus belongs to perennial herbaceous plants of the Cyperaceae, is a special species of coastal wetlands of Yangtze river and Hangzhou bay in China, is also an important food resource for overwintering and waiting birds, has important significance for maintaining biological diversity and protecting important biological habitats, and is an ideal species for ecological restoration of the coastal wetlands. However, its growth and propagation are limited by the supply of soil nutrients and physicochemical properties. The biochar is used as a high-efficiency soil conditioner, and can improve the carbon content of soil, improve the nutrient availability and promote the plant growth. The prior study shows that spartina alterniflora biochar has the potential of improving the soil of the coastal wetland, but the concentration dependency effect of spartina alterniflora on the growth and carbon fixation capacity of spartina alterniflora has not been systematically elucidated. Therefore, an optimization technology based on spartina alterniflora biochar is developed, so that the resource utilization of invasive plants can be realized, the ecological function of the wetland can be enhanced, and the method has important scientific and application values.|DISCLOSURE|Disclosure of Invention|[0005] The invention aims to solve the defects in the prior art, and provides a method for promoting the growth of the scirpus acutangus in the coastal wetland by utilizing the spartina alterniflora biochar, which is characterized in that the addition concentration of the biochar is optimized, improving the biomass, root development and propagation characteristics of the scirpus aculeatus, improving the soil environment, enhancing the carbon sequestration capacity of the wetland, and providing technical support for ecological restoration and carbon sequestration management.|[0006] In order to achieve the above purpose, the present invention adopts the following technical scheme:| the method for promoting the growth of the spartina alterniflora by utilizing spartina alterniflora biochar comprises the following steps: | S1, preparing biochar, namely collecting spartina alterniflora, naturally airing after cleaning, cutting into small sections below 5 cm, drying at 60 ℃, crushing by using a crusher, sieving by using a 60-mesh sieve, and performing anaerobic pyrolysis at 500 ℃ for 2 hours to prepare the biochar; |S2, soil treatment, namely collecting coastal wetland salt swamp soil, adding 0%, 0.5%, 1% and 3% of biochar according to the weight ratio, and fully and uniformly mixing with the soil to prepare different treatment groups; | S3, planting plants, namely selecting healthy scirpus seedlings, transplanting the scirpus seedlings into soil containing biochar, planting 24 plants in each container, keeping the soil moisture to be about 60% of the field water holding capacity, watering twice a week, and culturing for 9 months under the greenhouse condition; | and S4, growth management, namely periodically measuring plant biomass, root system morphology, propagation characteristics and soil indexes, and finally screening the 1% biochar adding concentration as the optimal scheme. |[0007] As a further technical scheme of the invention, in the step S2, the depth of the salt marsh soil of the collected coastal wetland is 0-10cm.|[0008] As a further technical scheme of the invention, in the S3, the height of the healthy scirpus seedling is 10-15cm, the root system is complete, and the size of a container for transplanting scirpus is 55cm multiplied by 40cm multiplied by 35cm.|[0009] As a further technical scheme of the invention, in the S3, the greenhouse condition is that the temperature is 25-30 ℃, the illumination intensity is 500 mu mol m -2s-1, and the humidity is 60-70%.|[0010] In the step S4, the plant biomass includes the ground and the underground, the root system form includes root length, root surface area and root volume, the propagation characteristics include seed number and bulb number, and the soil indexes include water content, pH, salinity, conductivity, nitrate nitrogen, ammonium nitrogen, available phosphorus, total nitrogen, total carbon and organic carbon.|[0011] As a further technical scheme of the invention, the 1% biochar addition concentration increases the total biomass of the scirpus by 35%, the overground biomass by 36.65%, the underground biomass by 115.04%, the root length by 135.84%, the soil nitrate nitrogen by 14.35%, the ammonium nitrogen by 26.84%, the available phosphorus by 20.15%, and the soil nutrient and nitrification rate are obviously optimized to be the optimal concentration.|[0012] As a further technical scheme of the invention, the method is suitable for coastal wetland ecological restoration, invasive plant resource utilization and blue carbon sink management, and can remarkably reduce the carbon reserve loss of the wetland.|[0013] The plant propagation strategy is optimized and the carbon fixation capacity is improved by enhancing the asexual propagation characteristics of scirpus (the number of bulbs is increased by 39.80%).|[0014] The beneficial effects of the invention are as follows:| 1. the plant growth is obviously promoted, 1 percent of biochar treatment obviously promotes the scirpus aculeatus biomass and root system development, and enhances the carbon fixation potential. |[0015] 2. Optimizing soil environment, raising water content, nutrient availability and nitration rate, and improving physical and chemical properties of salt marsh soil.|[0016] 3. And (3) recycling, namely converting spartina alterniflora into charcoal to realize the combination of invasive plant treatment and resource circulation.|[0017] 4. Ecological stability, namely avoiding salt accumulation and growth inhibition caused by high-concentration (3%) biochar, and ensuring application safety.|DRAWINGS DESCRIPTION|[0018] FIG. 1 is a flow chart of a method for promoting the growth of scirpus acutangus in the coastal wetland by utilizing spartina alterniflora biochar.|INVENTION MODE|Detailed Description|[0019] The invention is further described in connection with the following detailed description, in order to make the technical means, the creation characteristics, the achievement of the purpose and the effect of the invention easy to understand.|[0020] Referring to fig. 1, the method for promoting the growth of the spartina alterniflora in the coastal wetland by utilizing spartina alterniflora biochar comprises the following steps:| S1, preparing biochar, namely collecting spartina alterniflora, naturally airing after cleaning, cutting into small sections below 5 cm, drying at 60 ℃, crushing by using a crusher, sieving by using a 60-mesh sieve, and performing anaerobic pyrolysis at 500 ℃ for 2 hours to prepare the biochar; | S2, soil treatment, namely collecting coastal wetland salt swamp soil (depth is 0-10 cm), adding 0%, 0.5%, 1% and 3% of biochar according to weight ratio respectively, and fully and uniformly mixing with the soil to prepare different treatment groups; | S3, planting plants, namely selecting healthy scirpus seedlings (with the height of 10-15cm and complete root systems), transplanting the scirpus seedlings into soil containing biochar, planting 24 plants in each container (with the size of 55cm multiplied by 40cm multiplied by 35 cm), keeping the soil moisture to be about 60% of the field water holding capacity, watering twice a week, and culturing for 9 months under the greenhouse condition (the temperature of 25-30 ℃, the illumination intensity of 500 mu mol m -2s-1 and the humidity of 60-70 percent); | And S4, growing management, namely periodically measuring plant biomass (overground and underground), root morphology (root length, root surface area and root volume), propagation characteristics (seed number and bulb number), soil indexes (water content, pH, salinity, conductivity, nitrate nitrogen, ammonium nitrogen, available phosphorus, total nitrogen, total carbon and organic carbon), wherein the 1% biochar added concentration increases the total biomass of the scirpus with 35%, the overground biomass with 36.65%, the underground biomass with 115.04%, the root length with 135.84%, the soil nitrate nitrogen with 14.35%, the ammonium nitrogen with 26.84%, the available phosphorus with 20.15%, and the soil nutrient and nitrification rate are obviously optimized, so that the optimal concentration is obtained, and finally, the 1% biochar added concentration is selected as an optimal scheme. |[0021] In a preferred embodiment, the method is suitable for coastal wetland ecological restoration, invasive plant resource utilization and blue carbon sink management, and can remarkably reduce wetland carbon reserve loss.|[0022] The plant propagation strategy is optimized and the carbon fixation capacity is improved by enhancing the asexual propagation characteristics of scirpus (the number of bulbs is increased by 39.80%).|[0023] Example 1|S1, collecting spartina alterniflora in Hangzhou bay wetland (121 DEG 09'E,30 DEG 19' N), cleaning, naturally airing, cutting into small sections below 5 cm, drying at 60 ℃, crushing by using a crusher, sieving by using a 60-mesh sieve, and performing anaerobic pyrolysis at 500 ℃ for 2 hours to prepare biochar;| S2, taking Hangzhou Bay salt swamp soil, adding biochar according to 0%, 0.5%, 1% and 3%, uniformly mixing, and filling into a container; | S3, transplanting scirpus maritima seedlings (24 plants per container), and culturing in a greenhouse for 9 months (at 25-30 ℃ and under 500 mu mol m -2s-1 of illumination and 60-70% of humidity); | s4, after-harvest measurement, the result shows that the total biomass of the 1% treatment group is increased by 35%, the root length is increased by 135.84%, the nitrate nitrogen is increased by 14.35%, and the available phosphorus is increased by 20.15%. |[0024] Example 2|Based on example 1, biochar was prepared and the experiment was repeated with pyrolysis temperatures adjusted to 450 ℃ and 600 ℃, respectively. The result shows that the 500 ℃ pyrolytic biochar has the best effect in promoting the growth of scirpus aculeatus and improving the soil, and the stability of the technological parameters is verified.|[0025] From the above description, it can be seen that the above-described embodiments of the present invention achieve the technical effects of growth promotion by 1% biochar treatment to increase the scirpus overground biomass by 36.65%, underground biomass by 115.04%, and significant enhancement of root development.|[0026] And (3) soil optimization, namely improving the water content of the soil by 12.54%, maximizing the nitrification rate and improving the nutrient availability.|[0027] The ecological benefit is that the carbon fixation potential of the wetland is enhanced, and the resource utilization of invasive plants is realized.|[0028] The ecological stability is realized by systematically screening the optimal concentration (1%), so that salt accumulation and plant growth inhibition caused by high concentration (3%) are avoided, and a high-efficiency and feasible technical scheme is provided for the coastal wetland restoration.|[0029] It will be appreciated by persons skilled in the art that the foregoing discussion of any embodiment is merely exemplary and is not intended to imply that the scope of the invention (including the claims) is limited to these examples, that combinations of technical features in the foregoing embodiments or in different embodiments may be implemented in any order and that many other variations of the different aspects of the invention as described above may exist within the spirit of the invention, and that they are not provided in detail for clarity.|[0030] The present invention is intended to embrace all such alternatives, modifications and variances which fall within the broad scope of the appended claims. Therefore, any omission, modification, equivalent replacement, improvement, etc. of the present invention should be included in the scope of the present invention. (CN120188688)|TECHNICAL FIELD|Technical Field|[0001] The invention relates to the technical field of wetland ecology and carbon circulation, in particular to a method for promoting the growth of scirpus maritima in a coastal wetland by utilizing spartina alterniflora biochar, which is suitable for the ecological restoration of the coastal wetland, the resource utilization of invasive plants and the improvement of carbon sink functions.|BACKGROUND ART|[0002] Coastal wetlands are globally important ecosystems with the functions of maintaining biodiversity, regulating climate and storing "blue carbon". However, the invasion of spartina alterniflora has a versatile negative impact on the ecosystem. The rapid diffusion of the plant growth regulator is used for occupying the living space of the original plants, so that the degradation of the original vegetation community is caused, and the balance of biodiversity is destroyed. In addition, the dense growth of the spartina alterniflora also causes the blockage of a channel, influences water traffic and coastal economic activities, and threatens the health and functions of the coastal wetland ecosystem. The existing treatment method mostly adopts mechanical cleaning, but the situation is broken and the carbon warehouse is lost, so that the carbon fixing capacity of the wetland is weakened. Natural-based solutions are considered as effective ways to reestablish the ecological function of the wetland by native plant restoration and soil improvement.|[0003] The scirpus maritima is an ideal species for recovering the coastal wetland, and has remarkable significance for maintaining biodiversity and protecting key biological habitat due to the strong environment adaptability and the characteristic of being an important food resource of birds. However, its growth is limited by soil nutrients and physicochemical properties. The biochar is used as a soil conditioner, can improve the soil environment and promote plant growth, but the prior research has not systematically revealed the concentration dependency effect and carbon fixation mechanism of spartina alterniflora biochar on scirpus. Therefore, the development of the ecological restoration technology based on spartina alterniflora biochar has important significance.|[0004] The scirpus maritimus belongs to perennial herbaceous plants of the Cyperaceae, is a special species of coastal wetlands of Yangtze river and Hangzhou bay in China, is also an important food resource for overwintering and waiting birds, has important significance for maintaining biological diversity and protecting important biological habitats, and is an ideal species for ecological restoration of the coastal wetlands. However, its growth and propagation are limited by the supply of soil nutrients and physicochemical properties. The biochar is used as a high-efficiency soil conditioner, and can improve the carbon content of soil, improve the nutrient availability and promote the plant growth. The prior study shows that spartina alterniflora biochar has the potential of improving the soil of the coastal wetland, but the concentration dependency effect of spartina alterniflora on the growth and carbon fixation capacity of spartina alterniflora has not been systematically elucidated. Therefore, an optimization technology based on spartina alterniflora biochar is developed, so that the resource utilization of invasive plants can be realized, the ecological function of the wetland can be enhanced, and the method has important scientific and application values.|DISCLOSURE|Disclosure of Invention|[0005] The invention aims to solve the defects in the prior art, and provides a method for promoting the growth of the scirpus acutangus in the coastal wetland by utilizing the spartina alterniflora biochar, which is characterized in that the addition concentration of the biochar is optimized, improving the biomass, root development and propagation characteristics of the scirpus aculeatus, improving the soil environment, enhancing the carbon sequestration capacity of the wetland, and providing technical support for ecological restoration and carbon sequestration management.|[0006] In order to achieve the above purpose, the present invention adopts the following technical scheme:| the method for promoting the growth of the spartina alterniflora by utilizing spartina alterniflora biochar comprises the following steps: | S1, preparing biochar, namely collecting spartina alterniflora, naturally airing after cleaning, cutting into small sections below 5 cm, drying at 60 ℃, crushing by using a crusher, sieving by using a 60-mesh sieve, and performing anaerobic pyrolysis at 500 ℃ for 2 hours to prepare the biochar; |S2, soil treatment, namely collecting coastal wetland salt swamp soil, adding 0%, 0.5%, 1% and 3% of biochar according to the weight ratio, and fully and uniformly mixing with the soil to prepare different treatment groups; | S3, planting plants, namely selecting healthy scirpus seedlings, transplanting the scirpus seedlings into soil containing biochar, planting 24 plants in each container, keeping the soil moisture to be about 60% of the field water holding capacity, watering twice a week, and culturing for 9 months under the greenhouse condition; | and S4, growth management, namely periodically measuring plant biomass, root system morphology, propagation characteristics and soil indexes, and finally screening the 1% biochar adding concentration as the optimal scheme. |[0007] As a further technical scheme of the invention, in the step S2, the depth of the salt marsh soil of the collected coastal wetland is 0-10cm.|[0008] As a further technical scheme of the invention, in the S3, the height of the healthy scirpus seedling is 10-15cm, the root system is complete, and the size of a container for transplanting scirpus is 55cm multiplied by 40cm multiplied by 35cm.|[0009] As a further technical scheme of the invention, in the S3, the greenhouse condition is that the temperature is 25-30 ℃, the illumination intensity is 500 mu mol m -2s-1, and the humidity is 60-70%.|[0010] In the step S4, the plant biomass includes the ground and the underground, the root system form includes root length, root surface area and root volume, the propagation characteristics include seed number and bulb number, and the soil indexes include water content, pH, salinity, conductivity, nitrate nitrogen, ammonium nitrogen, available phosphorus, total nitrogen, total carbon and organic carbon.|[0011] As a further technical scheme of the invention, the 1% biochar addition concentration increases the total biomass of the scirpus by 35%, the overground biomass by 36.65%, the underground biomass by 115.04%, the root length by 135.84%, the soil nitrate nitrogen by 14.35%, the ammonium nitrogen by 26.84%, the available phosphorus by 20.15%, and the soil nutrient and nitrification rate are obviously optimized to be the optimal concentration.|[0012] As a further technical scheme of the invention, the method is suitable for coastal wetland ecological restoration, invasive plant resource utilization and blue carbon sink management, and can remarkably reduce the carbon reserve loss of the wetland.|[0013] The plant propagation strategy is optimized and the carbon fixation capacity is improved by enhancing the asexual propagation characteristics of scirpus (the number of bulbs is increased by 39.80%).|[0014] The beneficial effects of the invention are as follows:| 1. the plant growth is obviously promoted, 1 percent of biochar treatment obviously promotes the scirpus aculeatus biomass and root system development, and enhances the carbon fixation potential. |[0015] 2. Optimizing soil environment, raising water content, nutrient availability and nitration rate, and improving physical and chemical properties of salt marsh soil.|[0016] 3. And (3) recycling, namely converting spartina alterniflora into charcoal to realize the combination of invasive plant treatment and resource circulation.|[0017] 4. Ecological stability, namely avoiding salt accumulation and growth inhibition caused by high-concentration (3%) biochar, and ensuring application safety.|DRAWINGS DESCRIPTION|[0018] FIG. 1 is a flow chart of a method for promoting the growth of scirpus acutangus in the coastal wetland by utilizing spartina alterniflora biochar.|INVENTION MODE|Detailed Description|[0019] The invention is further described in connection with the following detailed description, in order to make the technical means, the creation characteristics, the achievement of the purpose and the effect of the invention easy to understand.|[0020] Referring to fig. 1, the method for promoting the growth of the spartina alterniflora in the coastal wetland by utilizing spartina alterniflora biochar comprises the following steps:| S1, preparing biochar, namely collecting spartina alterniflora, naturally airing after cleaning, cutting into small sections below 5 cm, drying at 60 ℃, crushing by using a crusher, sieving by using a 60-mesh sieve, and performing anaerobic pyrolysis at 500 ℃ for 2 hours to prepare the biochar; | S2, soil treatment, namely collecting coastal wetland salt swamp soil (depth is 0-10 cm), adding 0%, 0.5%, 1% and 3% of biochar according to weight ratio respectively, and fully and uniformly mixing with the soil to prepare different treatment groups; | S3, planting plants, namely selecting healthy scirpus seedlings (with the height of 10-15cm and complete root systems), transplanting the scirpus seedlings into soil containing biochar, planting 24 plants in each container (with the size of 55cm multiplied by 40cm multiplied by 35 cm), keeping the soil moisture to be about 60% of the field water holding capacity, watering twice a week, and culturing for 9 months under the greenhouse condition (the temperature of 25-30 ℃, the illumination intensity of 500 mu mol m -2s-1 and the humidity of 60-70 percent); | And S4, growing management, namely periodically measuring plant biomass (overground and underground), root morphology (root length, root surface area and root volume), propagation characteristics (seed number and bulb number), soil indexes (water content, pH, salinity, conductivity, nitrate nitrogen, ammonium nitrogen, available phosphorus, total nitrogen, total carbon and organic carbon), wherein the 1% biochar added concentration increases the total biomass of the scirpus with 35%, the overground biomass with 36.65%, the underground biomass with 115.04%, the root length with 135.84%, the soil nitrate nitrogen with 14.35%, the ammonium nitrogen with 26.84%, the available phosphorus with 20.15%, and the soil nutrient and nitrification rate are obviously optimized, so that the optimal concentration is obtained, and finally, the 1% biochar added concentration is selected as an optimal scheme. |[0021] In a preferred embodiment, the method is suitable for coastal wetland ecological restoration, invasive plant resource utilization and blue carbon sink management, and can remarkably reduce wetland carbon reserve loss.|[0022] The plant propagation strategy is optimized and the carbon fixation capacity is improved by enhancing the asexual propagation characteristics of scirpus (the number of bulbs is increased by 39.80%).|[0023] Example 1|S1, collecting spartina alterniflora in Hangzhou bay wetland (121 DEG 09'E,30 DEG 19' N), cleaning, naturally airing, cutting into small sections below 5 cm, drying at 60 ℃, crushing by using a crusher, sieving by using a 60-mesh sieve, and performing anaerobic pyrolysis at 500 ℃ for 2 hours to prepare biochar;| S2, taking Hangzhou Bay salt swamp soil, adding biochar according to 0%, 0.5%, 1% and 3%, uniformly mixing, and filling into a container; | S3, transplanting scirpus maritima seedlings (24 plants per container), and culturing in a greenhouse for 9 months (at 25-30 ℃ and under 500 mu mol m -2s-1 of illumination and 60-70% of humidity); | s4, after-harvest measurement, the result shows that the total biomass of the 1% treatment group is increased by 35%, the root length is increased by 135.84%, the nitrate nitrogen is increased by 14.35%, and the available phosphorus is increased by 20.15%. |[0024] Example 2|Based on example 1, biochar was prepared and the experiment was repeated with pyrolysis temperatures adjusted to 450 ℃ and 600 ℃, respectively. The result shows that the 500 ℃ pyrolytic biochar has the best effect in promoting the growth of scirpus aculeatus and improving the soil, and the stability of the technological parameters is verified.|[0025] From the above description, it can be seen that the above-described embodiments of the present invention achieve the technical effects of growth promotion by 1% biochar treatment to increase the scirpus overground biomass by 36.65%, underground biomass by 115.04%, and significant enhancement of root development.|[0026] And (3) soil optimization, namely improving the water content of the soil by 12.54%, maximizing the nitrification rate and improving the nutrient availability.|[0027] The ecological benefit is that the carbon fixation potential of the wetland is enhanced, and the resource utilization of invasive plants is realized.|[0028] The ecological stability is realized by systematically screening the optimal concentration (1%), so that salt accumulation and plant growth inhibition caused by high concentration (3%) are avoided, and a high-efficiency and feasible technical scheme is provided for the coastal wetland restoration.|[0029] It will be appreciated by persons skilled in the art that the foregoing discussion of any embodiment is merely exemplary and is not intended to imply that the scope of the invention (including the claims) is limited to these examples, that combinations of technical features in the foregoing embodiments or in different embodiments may be implemented in any order and that many other variations of the different aspects of the invention as described above may exist within the spirit of the invention, and that they are not provided in detail for clarity.|[0030] The present invention is intended to embrace all such alternatives, modifications and variances which fall within the broad scope of the appended claims. Therefore, any omission, modification, equivalent replacement, improvement, etc. of the present invention should be included in the scope of the present invention. Family Number|(115012249)|115012249|Abstract|(CN120188688 A)|The invention discloses a method for promoting the growth of coastal wetland scirpus mariqueter by using spartina alterniflora biochar , which comprises the following steps : S1 , collecting spartina alterniflora , cleaning , naturally airing , cutting into small sections of less than 5 cm , drying at 60 DEG C , crushing , sieving by a 60- mesh sieve , and performing anaerobic pyrolysis at 500 DEG C for 2 hours to prepare biochar ; s2 , coast wetland salt marsh soil is collected , 0%, 0.5%, 1% and 3% of biochar are added according to the weight ratio , and the biochar and the soil are mixed to be uniform to prepare different treatment groups ; s3 , healthy scirpus mariqueter seedlings are selected , transplanted into the soil containing the biochar and cultured for 9 months under the greenhouse condition ; s4 , regularly measuring plant biomass , root morphology , reproduction characteristics and soil indexes , and finally screening 1% biochar addition concentration as an optimal scheme ; according to the method , resource utilization of invasive plants is achieved , the wetland carbon sequestration potential is enhanced , and a scientific basis and an application approach are provided for coastal wetland ecological restoration and blue carbon sink management . |CPC codes|(CN120188688 A)|A01G - 022/00 |A01G - 024/10 |IPC codes|(CN120188688 A)|A01G - 022/00 |A01G - 024/10 | Basic materials chemistry|Other special machines A01G-022/00|A01G-024/10|C09K-017/02|C09K-2101/00 A01G-022/00|A01G-024/10|C09K-017/02|C09K-2101/00 A01G-022/00|A01G-024/10|C09K-017/02|C09K-101/00 A01G-022/00|A01G-024/10|C09K-017/02|C09K-101/00 PENDING (CN120188688)|PENDING ALIVE (CN120188688)|ALIVE (CN120188688)|LEGAL DETAILS FOR CN120188688|Actual or expected expiration date=2045-03-27|Legal state=ALIVE|Status=PENDING|Event publication date=2025-03-27|Event code=CN/APP|Event indicator=Pos|Event group=Examination events|Application details|Application country=CN CN202510370583|Application date=2025-03-27|Standardized application number=2025CN-0370583|Event publication date=2025-06-24|Event code=CN/A|Event group=Examination events|Published application|Publication country=CN|Publication number=CN120188688|Publication stage code=A|Publication date=2025-06-24|Standardized publication number=CN120188688|Event publication date=2025-06-24|Event code=CN/PB01|Event group=Examination events|Publication|Event publication date=2025-07-11|Event code=CN/SE01|Event group=Examination events|Entry into substantive examination (CN120188688)|CN https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfkemQIFgum+Ffn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1 https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000077927717&ekey=2209&xpn=CN120188688&kind=A https://pss-system.cponline.cnipa.gov.cn/conventionalSearch https://permalink.orbit.com/RenderStaticFirstPage?XPN=0hpoXhIqVLWcQDRFQTPvH5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT CN (CN120188688)|CN (CN120188688)|NAME=RESEARCH INSTITUTE OF SUBTROPICAL FORESTRY CHINESE ACADEMY OF FORESTRY , COUNTRY=CN (CN120188688)|NAME=LIU HUIMIN;BEIJING JUNTAI-MIZUKI INTELLECTUAL PROPERTY AGENCY LTD. , REG=11906 (CN120188688)|NAME=LI NIU|NAME=WU MING|NAME=SHAO XUEXIN|NAME=TANG YAOYAO|NAME=JIANG PENGCHENG|NAME=GAO JINGWEN 0 1 Titre: (CN120188688)|Method for promoting growth of coastal wetland scirpus mariqueter by using spartina alterniflora charcoal Résumé: (CN120188688)|The invention discloses a method for promoting the growth of coastal wetland scirpus mariqueter by using spartina alterniflora biochar, which comprises the following steps: S1, collecting spartina alterniflora, cleaning, naturally airing, cutting into small sections of less than 5 cm, drying at 60 DEG C, crushing, sieving by a 60-mesh sieve, and performing anaerobic pyrolysis at 500 DEG C for 2 hours to prepare biochar; s2, coast wetland salt marsh soil is collected, 0%, 0.5%, 1% and 3% of biochar are added according to the weight ratio, and the biochar and the soil are mixed to be uniform to prepare different treatment groups; s3, healthy scirpus mariqueter seedlings are selected, transplanted into the soil containing the biochar and cultured for 9 months under the greenhouse condition; s4, regularly measuring plant biomass, root morphology, reproduction characteristics and soil indexes, and finally screening 1% biochar addition concentration as an optimal scheme; according to the method, resource utilization of invasive plants is achieved, the wetland carbon sequestration potential is enhanced, and a scientific basis and an application approach are provided for coastal wetland ecological restoration and blue carbon sink management. 123 Abstract gpt-4o-mini no The article focuses on using biochar from invasive plants to promote plant growth and enhance carbon sequestration in coastal wetlands, but it does not involve accelerated weathering of minerals or direct CO₂ capture processes.
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